Process for Preparing a Water Continuous Emulsion From Heavy Crude Fraction

This invention is related to the production of oil-in-water emulsion(s). More specifically, this invention provides a process for the production of oil-in-water emulsions(s), especially for pipeline transmission and for burning.

The formulation of pipeline-transportable crude oil-in-water emulsion can not generally be formulated by combining emulsifying agent(s) directly with produced hydrocarbon crude, and subsequently agitating with a dynamic mixer the mixture of produced hydrocarbon crude and emulsifying agent(s). The emulsifying agent(s) is not soluble in oil and is only soluble in an aqueous solution. By contacting directly the produced hydrocarbon crude with the emulsifying agent(s) without premixing the emulsifying agent(s) with water, brine, or the like, diffusion of the emulsifying interface is slow; and with some produced hydrocarbon crudes, such as Athabasca bitumen from the Athabasca tar sands in the province of Alberta, Canada, oil-in-water emulsion(s) can not be formulated. Also, through the use of a dynamic mixer, such as the rotor-stator mixer, not every produced hydrocarbon crude can be emulsified into a water continuous emulsion, even with premixing the emulsifying agent(s) with water prior to combining with produced hydrocarbon crude. A high shear field cannot be obtained with a dynamic mixer unless the mixture of produced hydrocarbon crude and emulsifying agent(s) (including any water solvent) makes numerous passes through the dynamic mixer. Transport oil-in-water emulsion(s) is shear-sensitive, and a dynamic mixer tends to cause either an overshear-damaged product or less than a perfectly mixed product, depending on the mixing severity employed with the dynamic mixer.

Large storage tanks and/or mixing tanks are generally required when utilizing dynamic mixers. If a dynamic mixer is separate from the storage tank, mixtures to be emulsified have to be recirculated from the storage tank, through the mixer, and back into the storage tank. The degree of mixing achieved by dynamic mixers depends on the mixing speed, impeller design, impeller position, length of mixing time, tank volume, tank geometry, etc. Dynamic mixers are prone to producing a large quantity of oil droplets having a diameter of less than 10 micron, which is detrimental to the transport of oil-in-water emulsion(s) as such small oil droplet increase the viscosity of the oil-in-water emulsion(s), and can cause the oil-in-water emulsion(s) to invert from a water continuous emulsion into an oil continuous emulsion, with an attendant increase in viscosity. Dynamic mixers are also susceptible to high maintenance expense because of their use of high-speed rotating devices.

What is needed and what has been invented by us is a process for the preparation of stable water-continuous crude oil, or other hydrocarbon, transport emulsions, and which can generally form an emulsion having a water-continuous phase of any produced hydrocarbon crude, especially Athabasca bitumen (e.g. Syncrude bitumen) from the Athabasca tar sands in the province of Alberta, Canada.

It is therefore an object of this invention to provide a process for the preparation of a stable oil-in-water emulsion(s).

It is another object of this invention to provide a process for the preparation of a stable oil-in-water emulsion(s) with the use of a static mixer.

It is yet another object of this invention to provide a process for the preparation of a stable oil-in-water emulsion(s) that is pipeline-transportable.

Still other objects will be apparent to those skilled in the art from the following description of this invention.

The foregoing objects are achieved according to the practice of this invention. Broadly, this invention comprises a process for the production of an oil-in-water emulsion that are particularly useful for pipeline transmission. The process comprises mixing a hydrocarbon with an emulsifying composition(s) which comprises water and an emulsifying agent(s) to produce an oil-in-water emulsion when the temperature of the mixture of hydrocarbon and emulsifying composition(s) is from about 100.degree. F. to about 200.degree. F. The amount of the emulsifying composition(s) that is mixed with the hydrocarbon is sufficient to form an oil-in-water emulsion having a selected water content of from about 15 percent to about 60 percent by weight water and a viscosity sufficiently low for pipeline transmission. The process additionally comprises shearing and mixing statically the mixture of hydrocarbon and emulsifying composition(s) when the mixture is at a temperature of from about 100.degree. F. to about 200.degree. F. to form an oil-in-water emulsion.

The hydrocarbon may be any hydrocarbon or hydrocarbon crude, or any fractionated or extracted part(s) thereof, that has a gravity of from about -6 degree API to about 23 degree API, preferably from about 5 degree API to about 15 degree API, and with which it is desired to formulate an oil-in-water emulsion(s) for any use, especially in order to facilitate the transmission or transportation of the hydrocarbon or hydrocarbon crude, or any fractionated or extracted part(s) thereof, through a pipeline, or the like. The hydrocarbon may be any of those hydrocarbons that have been typically termed atmospheric bottoms, vacuum bottoms, vacuum residuals, deasphalter bottoms, etc. Thus, whenever "hydrocarbon" and/or "hydrocarbon crude" is referred to herein, "hydrocarbon" and/or "hydrocarbon crude" is to be construed to mean any hydrocarbon or hydrocarbon crude, or any fractionated or extracted part(s) thereof, which is capable of forming with the emulsifying composition(s) of this invention, a stable oil-in-water emulsion. The formed oil-in-water emulsion may be employed for any suitable use including, but not limited to, burning in a boiler (or burner), transporting through a pipeline, etc.

The emulsifying composition(s) of this invention comprises an emulsifying agent selected from the compounds having the general formula: ##STR1## where n is from about 7 to about 20 and y is from about 4 to about 1000; or ##STR2## where n.sub.1 is from about 7 to about 18, n.sub.2 is from about 7 to about 18, and y.sub.1 is from about 4 to about 1000. In compound(s) (1) and/or compound(s) (2), each of y and y.sub.1 is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s) which is the mean of a normal Gaussian distribution curve. The hexagon with a circle in the center in compound(s) (1) and/or compound(s) (2), and throughout this specification and in the claims, represents a benzene ring.

A mixture of compound(s) (1) and compound(s) (2) may be employed. Depending on the particular emulsifying agent(s), the concentration of the emulsifying agent(s) employed may range from about 25 to about 15,000 ppm by weight of the hydrocarbon. The amount of the emulsifying agent(s) employed is preferably just sufficient to stabilize an oil-in-water emulsion or an oil-in-aqueous phase emulsion at a 15% by wt. to about 60% by wt. water-content or aqueous phase content.

The formulated oil-in-water emulsion(s) of this invention can be transported through a pipeline. If a proportion of the disperse oil droplet phase in the oil-in-water emulsion(s) at least partially coalesces in the water continuous phase to produce a mixture comprising the coalesced oil droplet phase and residual oil-in-water emulsion, the mixture may be further transported through the same pipeline, even without removing the mixture for treatment or reformulation of the original oil-in-water emulsion(s). It has been discovered that the mixture has a viscosity less than or equal to the viscosity of the originally formulated oil-in-water emulsion in spite of the fact that the at least partially coalesced oil droplet phase has a viscosity larger than the viscosity of the originally formulated oil-in-water emulsion(s). It has also been discovered that a substantial proportion of the originally formulated oil-in-water emulsion does not invert into a water-in-oil emulsion when the oil droplets within the originally formulated oil-in-water emulsion coalesce to produce a water continuous mixture comprising the coalesced oil droplets, and residual oil-in-water emulsion which is the remaining oil-in-water emulsion from the originally formulated oil-in-water emulsion and contains oil droplets that have not coalesced.

FIG. 1 is a schematic flow diagram of an embodiment of the process for the preparation of stable oil-in-water emulsion(s);

FIG. 2 is a schematic flow diagram illustrating a pair of static mixing devices in parallel;

FIG. 3 is a schematic flow diagram disclosing a pump and a static mixing device for producing or reproducing a multimodal oil-in-water emulsion(s);

FIG. 4 is a partially cut-away perspective view of one embodiment of the static mixing device for the present invention;

FIG. 5 is a perspective view of one baffle element for the static mixing device of FIG. 4;

FIG. 6 is a perspective view of another baffle element for the static mixing device of FIG. 4;

FIG. 7 is a cut-away plan view of the static mixing device of FIG. 4;

FIG. 8 is a partially cut-away perspective view of another embodiment of the static mixing device for the present invention;

FIG. 9 is a partial perspective view of three interconnected baffle elements for the static mixing device of FIG. 8;

FIG. 10 is a partial perspective view of a baffle element for the static mixing device of FIG. 8 with the direction of the arrows representing back-mixing action for the mixture of produced hydrocarbon crude and emulsifying composition(s);

FIG. 11 is a partial perspective view of the baffle element for the static mixing device of FIG. 8 with the direction of the arrows representing a splitting action for the mixture of produced hydrocarbon crude and emulsifying composition(s);

FIG. 12 is a partial perspective view of the baffle element for the static mixing device of FIG. 8 with the direction of the arrows representing cross-current mixing action for the mixture of produced hydrocarbon crude and emulsifying composition(s);

FIG. 13 is a partial perspective view of another embodiment of an end of the baffle element for the static mixing device of FIG. 8;

FIG. 14 is a partially cut-away perspective view of yet another embodiment of the static mixing device for the present invention;

FIG. 15 is a top plan view of one of the baffle elements for the static mixing device of FIG. 13;

FIG. 16 is an elevational view of an embodiment of an apparatus for forming a downhole oil-in-aqueous phase emulsion;

FIG. 17 is a partial enlarged elevational view of the apparatus of FIG. 16;

FIG. 18 is an elevational view of an embodiment of an apparatus which continuously injects an emulsifying composition downhole to form a downhole oil-in-aqueous phase emulsion;

FIG. 19 is an elevational view of an embodiment of an apparatus which batch injects an emulsifying composition downhole to form a downhole oil-in-aqueous phase emulsion; and

FIG. 20 is an elevational view of another embodiment of the apparatus of FIGS. 18 and 19 for forming downhole an oil-in-aqueous phase emulsion;

FIG. 21 is a graph of the effect of temperature on asphalt WCE;

FIG. 22 is a graph of the effect of certain additives on the static stability of asphalt emulsions after being stored 4 days;

FIG. 23 is a graph of the effect of xanthan concentration on the static stability of asphalt emulsions after being stored a week;

FIG. 24 is a graph of the effect of xanthan on the static stability of finished asphalt emulsions after being stored one week;

FIG. 25 is a schematic diagram of asphalt emulsion preparation and skim handling;

FIG. 26 is a microscopic diagram of an oil continuous emulsion comprising 10% water, NP-9 additive; and

FIG. 27 is a microscopic diagram of a double water-continuous emulsion 10% water in oil phase.

Referring in detail now to the drawings, and initially more particularly to FIG. 1, a stream of hydrocarbon crude is produced from a source and is transported into a crude oil tank 10 through a conduit 12. A valve 14 within the conduit 12 controls the flow of the crude through the same. The hydrocarbon crude may be any hydrocarbon and/or hydrocarbon crude, or any fractionated or extracted part(s) thereof, that preferably has a gravity of from about -6 degree API to about 23 degree API.

The source of the produced hydrocarbon crude may be any source wherefrom a hydrocarbon crude may be obtained, produced, or the like. The source may be one or more producing wells in fluid communication with a subterranean oil reservoir. The producing well(s) may be under thermal recovery conditions, or the producing well(s) may be in a heavy oil field where the hydrocarbon crude or oil is being produced from a reservoir having a strong water-drive. Generally, hydrocarbon crude produced from producing well(s) under a strong water-drive include high water-cuts, and appropriate artificial lift systems (e.g. submersible electrical pumps) are employed to assist the flow of the hydrocarbon crude because of its high water content. As will be discussed in greater detail hereinafter, this invention is particularly suitable for when the source of the produced hydrocarbon crude is from the Athabasca tar sands in the province of Alberta, Canada. Hydrocarbon crude from this source has generally been termed "Athabasca bitumen". No matter what the source is for the stream of produced hydrocarbon crude, the crude may essentially contain no water, or it may include water in various forms. The produced crude may also include some associated gas. For the purposes of the present invention, it will be assumed that the stream of produced hydrocarbon crude has a low gas/oil ratio (i.e. less than about 10% by wt. of C.sub.1 -C.sub.5).

Any water present in the stream of produced hydrocarbon crude can be classified into two categories: "bound" water and "free" water. "Bound" water is that water which is locked up as water-in-oil emulsion(s) that may be contained in the produced hydrocarbon crude. Separating "bound" water from the produced hydrocarbon crude typically requires applying the appropriate combination of heat, mixing and chemical additive(s). "Free" water is that water which is relatively loosely held up by the produced hydrocarbon crude and can be removed by merely heating the produced hydrocarbon crude to an appropriate temperature or providing sufficient residence time in tankage. The quantity of "free" water which can be removed will depend upon the temperature to which the stream of produced hydrocarbon crude is heated.

In the event that the stream of produced hydrocarbon crude contains a substantial amount of water-in-oil emulsion(s) and/or "free" water and/or associated gas, the crude may be fed into a "free" water knock-out unit (FWKO) 16 through a conduit 18 that includes a valve 20 to regulate and control the flow of the crude. To accomplish this change in direction of flow of the produced hydrocarbon crude, valve 20 in conduit 18 is opened, and valve 14 in conduit 12 is closed. The FWKO 16 is an optional piece of equipment and is not mandatory with respect to this invention, especially when Athabasca bitumen is being processed to formulate an oil-in-water emulsion for pipeline transportation. Athabasca bitumen contains essentially no associated gases and no water in any form, such as "free" water and/or water-in-oil emulsion(s) wherein the contained water is "bound" water.

To accomplish the purposes of this invention, the stream of produced hydrocarbon crude may by-pass the FWKO 16, even if one produced crude contains water-in-oil emulsion(s) and/or "free" water and/or associated gas. The stream of produced hydrocarbon crude can contain an oil/water mixture in any proportion. Pipeline-transportable oil-in-water emulsion(s) may be formulated in accordance with the principles of this invention by directly converting, changing or altering, or the like, a substantial part of a stream of produced hydrocarbon crude of water-in-oil emulsion(s), with or without "free" water and with or without associated gases, into pipeline-transportable oil-in-water emulsion(s). However, to facilitate the formulation of such pipeline-transportable oil-in-water emulsion(s), there may be occasions where it is desirable to use the FWKO 16, such as when the produced hydrocarbon crude contains extremely high cuts of "free" water and/or associated gases.

The FWKO 16 may be operated under pressure and has a heating unit 22 in it which allows the stream of produced hydrocarbon crude to be heated to any pre-set temperature within the unit design constraints in order to assist in removal of "free" water and/or associated gas. In some instances the stream of produced hydrocarbon crude enters the FWKO 16 at a high enough temperature so that the heating unit 22 does not have to be energized. In the FWKO 16, depending on the temperature, a portion or substantially all of the "free" water will be removed from the stream of produced hydrocarbon crude, and can be drained and/or transmitted from the FWKO 16 through a conduit 24 to a water tank 26, which is also in communication with a source of water, brine, or aqueous phase, or the like, through a conduit 28. This water, brine, or the like, provides the aqueous phase with which the emulsifying agent(s) of this invention can be mixed to produce the emulsifying composition(s) of this invention. Any associated gases co-produced with the produced hydrocarbon crude generally should separate from the stream of produced hydrocarbon crude in the FWKO 16 and vent through a conduit 30 which includes a valve 32. The separated associated gases may be transmitted for further use, or otherwise disposed.

The effluent from the FWKO 16 may be essentially a mixture of water-in-oil emulsion(s) and residual "free" water, if any. The effluent exits the FWKO 16 through a conduit 34 which is in communication with the conduit 12, as illustrated in FIG. 1. Conduit 34 contains a valve 36 which controls and regulates the flow of the effluent from the FWKO 16 through conduit 34 and into where it is transported into the crude oil tank 10. It should be re-emphasized that the stream of produced hydrocarbon crude may be essentially void of any of the various forms of water and/or gases, and may not and does not have to include any water-in-oil emulsion(s) and/or "free" water and/or associated gas for the features of this invention to produce or formulate a pipeline-transportable oil-in-water emulsion(s) by directly converting, changing, or altering the stream of produced hydrocarbon crude. The emulsifying composition(s) of this invention in combination with other features, will generally produce pipeline-transportable oil-in-water emulsion(s) regardless of any water-in-oil emulsion(s) and/or "free" water and/or associated gases contained within the stream of produced hydrocarbon crude.

Crude oil tank 10 has a temperature indicator 38 which monitors the temperature of the produced hydrocarbon crude. Crude oil tank 10 also includes a drain 40 which can drain off to a sump (not shown in the drawings) extra water (if desired) which settles to the bottom of the crude oil tank 10. When pipeline-transportable oil-in-water emulsion is to be formed in accordance with the principles of this invention, a valve 42 in a conduit 44 which is in communication with the crude oil tank 10, is opened and a crude oil pump 46 may be energized to transport produced hydrocarbon crude through a conduit 48 for eventual mixing, commingling, adding, or the like, with the emulsifying composition(s) at the entrance of a conduit 50. It should be understood that while the mixing or adding of the produced hydrocarbon crude with the emulsifying composition(s) is being represented as taking place at the entrance of conduit 50, other systems and/or means of mixing or adding together the produced hydrocarbon crude with the emulsifying composition(s) are within the spirit and scope of this invention. For example, if conduit 50 is a straight line extension of conduit 48 and integral therewith such that conduit 48 does not have a separate identity, the emulsifying composition(s) would be introduced into the conduit 48, either normal to or angular therewith. Likewise, a pump [preferably a rotating (e.g. centrifugal) pump] may be positioned in conduit 50 to further or additionally mix the produced hydrocarbon crude with the emulsifying composition(s).

As the produced hydrocarbon crude is being pumped by pump 46 through the conduit 48, it passes through a heat exchanger 52 to either heat or cool the crude to a temperature such that when the produced hydrocarbon crude is mixed with or added to the emulsifying composition(s), the temperature of the crude-emulsifying composition(s) mixture is from about 100.degree. F. to about 200.degree. F., preferably from about 130.degree. F. to about 170.degree. F., as the pipeline-transportable oil-in-water emulsion(s) is to be formed at these temperatures. It is the temperature of the mixture of the produced hydrocarbon crude plus emulsifying composition(s) that should be at a temperature of from about 100.degree. F. to about 200.degree. F., and not the produced hydrocarbon crude alone. Certain produced hydrocarbon crudes, such as Athabasca bitumen from the Athabasca tar sands, may have a temperature well above 200.degree. F. as it is being processed from the crude oil tank 10. In those instances, and depending on the temperature of the emulsifying composition(s), the heat exchanger 52 may function as a cooling unit to cool down the crude such that the crude-emulsifying composition(s) mixture would possess the required temperature (i.e. from about 100.degree. F. to about 200.degree. F. as previously indicated) to formulate the oil-in-water emulsion(s). Obviously, whether the heat exchanger 52 cools or heats the produced hydrocarbon crude would depend on the temperature of the emulsifying composition(s).

Temperature indicator 54 monitors the temperature of the stream of produced hydrocarbon crude as it exits heat exchanger 52 and flows through conduit 48. The rate of flow through conduit 48 is monitored either by a meter 56 and/or the pumping speed of pump 46. Meter 56 may also include a cut monitor and a sampler to monitor the composition of the stream of hydrocarbon crude with respect to "free" water content, water-in-oil emulsion(s), and associated gases.

The emulsifying composition(s) is formed or produced in the emulsifying composition tank 58 (hereinafter referred to only as "tank 58") which comprises a temperature indicator 60 to monitor the temperature of the emulsifying composition(s) and a mixer means 62 to homogenize and maintain homogenized the emulsifying composition(s). The emulsifying composition(s) of this invention comprises at least one emulsifying agent(s); water, brine, or the like, which hereinafter will be referred to only as "water"; and, optionally, a compound that lowers the freezing point of water, preferably ethylene glycol, in order to lower the freezing point of the emulsifying composition(s) and the eventually formed pipeline-transportable oil-in-water emulsion(s). Other compounds that may be employed to lower the freezing point of water include, but are not limited to, glycerol, propylene glycol, and various sugars, etc., and fall within the spirit and scope of this invention.

The emulsifying agent(s) of this invention is introduced into an emulsifying tank 64 through a conduit 66, and is dispensed into tank 58 through a conduit 68. Conduit 68 includes a valve 70 and a flow-meter 72 to regulate and meter, respectively, the flow of the emulsifying agent(s) through the conduit 68. The amount of emulsifying agent(s) used in the present invention may range from about 25 (or less) to about 10,000 (or more) ppm weight-to-weight of the produced hydrocarbon crude, preferably from about 300 to about 10,000 ppm by weight. Stated alternately, the emulsifying composition(s) preferably comprises from about 0.05 vol. % to about 4.0 vol. % of the emulsifying agent(s).

If the produced hydrocarbon crude bypasses the FWKO 16, the actual water-content of the produced hydrocarbon crude may vary widely. The produced hydrocarbon crude may contain up to about 95% by volume water, or it may be a relatively dry oil containing less than the amount of water required to form a low viscosity oil-in-water emulsion that is pipeline-pumpable. The object is to provide an oil-in-water emulsion containing from about 15% by weight to about 60% by weight water, preferably from about 25% by weight to about 35% by weight water. To accomplish this objective, water tank 26 is used to furnish water to tank 58. This water may be recovered from the as-received stream of produced hydrocarbon crude by separation in FWKO 16 (which is optional), or may be water externally derived from a source which is introduced into water tank 26 through conduit 28. The amount of emulsifying agent(s) added from emulsifier tank 64 is controlled so as to form a generally stable oil-in-water emulsion with an emulsifying agent(s) concentration suited for low-viscosity pipeline pumping. Any extra water will be loosely bound and should separate easily. Excess emulsifying agent(s) is expensive and should be avoided The introduction of too little emulsifying agent(s) is to be also avoided because an oil-in-water emulsion will not form suitable for pipeline transportation. However, the employment of too little emulsifier agent(s), or not enough emulsifier agent(s) for transportation through a long pipeline (such as over 1,000 miles long), is not critical because one of the features of this invention is that although the formulated oil-in-water emulsion may fail and/or breakdown in a pipeline into a mixture comprising an at least partially (i.e. partially or substantially) coalesced oil droplet phase and residual oil-in-water emulsion, the resulting mixture has a viscosity that is less than or equal to the viscosity of the original oil-in-water emulsion(s) notwithstanding the fact that the at leas partially coalesced oil droplet phase itself has a viscosity larger than the viscosity of the original oil-in-water emulsion(s). An attendant feature to this feature of the invention is that if and when the oil-in-water emulsion(s) of this invention fails or breaksdown in a pipeline into the mixture comprising an at least partially coalesced oil droplets and residual oil-in-water emulsion(s), it is done so without a substantial proportion of the formulated oil-in-water emulsion(s) being inverted into a water-in-oil emulsion. These features enable the mixture of coalesced oil droplets and residual oil-in-water emulsion to be continuously transported through the pipeline without having to remove the mixture to reformulate the oil-in-water emulsion(s).

A conduit 74 transports water from the water tank 26 into the tank 58 wherein water and the emulsifying agent(s) are mixed or combined together into the emulsifying composition(s). The pH of the emulifying composition(s) in tank 58 may be modified by chemical addition. A filter (not shown in the drawings) may be installed in conduit 74 to remove sediment. A valve 76 and a flow meter 78 are in conduit 74 to control and meter, respectively, the flow of the water. It is important that the emulsifying agent(s) of this invention be mixed or combined with water such that the emulsifying composition(s) contain water. If water is absent from the emulsifying composition(s), and the emulsifying agent(s) in a pure or relatively pure state contacts and/or mixes with the produced hydrocarbon crude, a pipeline-transportable oil-in-water emulsion(s) cannot be produced or formulated, even if water is added separately to the produced hydrocarbon crude, or the crude contains water in any of its various forms. The emulsifying agent(s) of this invention is essentially insoluble in hydrocarbon crude and would not form a homogeneous solution with the hydrocarbon crude. Also, unless water is present with the emulsifying agent(s) of this invention, diffusion of the emulsifying agent(s) through the hydrocarbon crude to the interface of the crude and water (which was separately added or already contained within the crude) is much too slow, if it occurs at all. This is especially true for Athabasca bitumen. Therefore, one of the salient features of this invention is the mixing of the emulsifying agent(s) with water prior to any emulsifying agent(s) contacting the produced hydrocarbon crude.

As was previously mentioned, a suitable freezing point depressant may be mixed with the water to lower the freezing point of the water and/or the emulsifying composition(s) and/or the eventually formed oil-in-water emulsions(s). For the purposes of illustrating this invention, ethylene glycol will be employed as the freezing point depressant. To accomplish the mixing of water with ethylene glycol, conduit 82 supplies an ethylene glycol tank 80 with ethylene glycol. Ethylene glycol can be introduced directly into the water tank 26 through a conduit 84 that contains a valve 86 for regulating the flow of ethylene glycol therethrough. A flow meter 88 is also provided within conduit 84 to monitor the direct flow of ethylene glycol into the water tank 26. Alternatively, ethylene glycol can be introduced directly through a conduit 90 into water that is flowing within conduit 74 from the water tank 26. Similarly to conduit 84, conduit 90 is provided with a valve 92 and a flow meter 93 to regulate and meter, respectively, the flow of ethylene glycol through conduit 90. To effect the flow of ethylene glycol through conduit 84, valve 86 in conduit 84 is opened and valve 92 in conduit 90 is closed; and to effect the flow of ethylene glycol through conduit 90, valve 92 in conduit 90 is opened and valve 86 in conduit 84 is closed. Optionally, to accomplish the purpose for using ethylene glycol, instead of introducing and mixing directly the ethylene glycol with the water, ethylene glycol may be introduced into and mixed directly with the emulsifying agent(s), or with the mixture of water and emulsifying agent(s) within the tank 58.

The emulsifying composition(s) of this invention is pumped out of tank 58 through a conduit 94 by an emulsifying composition pump 96. Before commencing the pumping of the emulsifying composition(s) through the conduit 94 with the pump 96, valve 98 at the bottom of the tank 58 and within the conduit 94 is opened. Emulsifier composition pump 96 further pumps or transports the emulsifying composition(s) through a conduit 100 to meet with, combine or mix with, or the like, the stream of produced hydrocarbon crude at the entrance of the conduit 50. Conduit 100 is provided with a flow meter 102 to monitor and indicate the flow of the emulsifying composition(s) en route to its meeting with the produced hydrocarbon crude. Conduit 100 passes through a heat exchanger 104 which is provided in order to control and provide the emulsifying composition(s) with a sufficient temperature such that when it meets and mixes with the produced hydrocarbon crude at the entrance to conduit 50, the temperature of the mixture of emulsifying composition(s) and produced hydrocarbon crude within conduit 50 is from about 100.degree. F. to about 200.degree. F. As was previously indicated, maintaining the temperature of the mixture of emulsifying composition(s) and produced hydrocarbon crude from about 100.degree. F. to about 200.degree. F. is important in order to form the oil-in-water emulsion(s), as well as to produce and/or maintain a viscosity of the mixture that enables the mixture to be pumped or transported through a pipeline. This is especially true when the produced hydrocarbon crude is Athabasca bitumen which may at times possess a temperature above 200.degree. F. and/or a high viscosity (e.g. 20,000 cp at about 100.degree. F.) that would render it difficult to pump or transport through a pipeline. Thus, heat exchanger 104, depending on the temperature of the produced hydrocarbon crude at the temperature indicator 54 and/or the temperature of emulsifying composition(s) from tank 58, may at times have to heat the emulsifying composition(s); at other times may have to cool the emulsifier composition(s) instead of heating it, in order that the mixture of produced hydrocarbon crude and emulsifying composition(s) possesses the appropriate temperature of from about 100.degree. F. to about 200.degree. F.; more preferably from about 160.degree. F. to about 195.degree. F. when the produced hydrocarbon crude is Athabasca bitumen because of the high viscosity factor of the Athabasca bitumen.

The pressure drop across the mixer is monitored as it travels through conduit 50 by a pressure and flow meter monitor 106. Conduit 50 leads or terminates into a static shearing and static mixing means or device, generally illustrated as 108, which produces the oil-in-water emulsion(s) when the mixture is passed at a certain velocity therethrough and at the temperature of from about 100.degree. F. to about 200.degree. F. In a preferred embodiment of the invention, the device 108 is not preceded or followed by any dynamic shearing and mixing device (such as in-line blenders, rotor-stator, homogenizer, etc.) because the quality of the produced oil-in-water emulsion(s) may be affected if sheared and/or mixed dynamically, especially for certain species of emulsifier agent(s) which will be more fully set forth hereinafter. With respect to these certain species of emulsifier agent(s) when used to formulate oil-in-water emulsion(s) with dynamic mixing and/or dynamic shearing, such formulated oil-in-water emulsions(s) tend to fail and/or breakdown into the previously indicated mixture comprising an at least partially (i.e. partially or substantially) coalesced oil droplets in the water continuous phase, and residual oil-in-water emulsion. As was previously mentioned, not withstanding such failure and/or breakdown, the resulting coalesced oil droplets-residual emulsion mixture would still have a viscosity less than or equal to the original oil-in-water emulsion(s). Therefore, such mixture may be continually transported or pumped through a pipeline, or the like, without any concerns for non-effective pipeline-viscosity that may have resulted from the failure and/or breakdown due to dynamic shearing and/or dynamic mixing. The effectiveness of other species of the emulsifier agent(s) of this invention is not affected by any form or means of agitation, including but not limited to dynamic shearing and/or dynamic mixing. Thus, while static shearing and/or static mixing may be a preferred means for formulating the oil-in-water emulsion(s) of this invention, dynamic shearing and/or dynamic mixing is within the spirit and scope of this invention for certain embodiments thereof.

The velocity of the mixture of produced hydrocarbon crude and emulsifying composition(s) through the static shearing and static mixing device 108 may be any suitable velocity as the oil-in-water emulsion(s) of the present invention may be formed or produced under laminar or turbulent flow conditions. However, in preferred embodiment of the present invention, crude oil pump 46 and emulsification composition pump 96 should be fixed or set such that when the mixture of emulsifying composition(s) and produced hydrocarbon crude enters the static shearing and static mixing device 108, the velocity of the mixture is from about 20 in./sec. to about 140 in./sec., more preferably from about 35 in./sec., to about 115 in./sec. The viscosity of the mixture may be any viscosity that enables the mixture to be pumped, but is preferably from about 100 cp. to about 10,000 cp. At a velocity ranging from about 20 in./sec. to about 140 in./sec., and depending on the viscosity of the mixture, the pressure drop across the mixture within conduit 50 is from about 10 psi. to about 150 psi., preferably from about 20 psi. to about 60 psi.

The static shearing and static mixing device 108 simultaneously shears and mixes the mixture of emulsifying composition(s) and the produced hydrocarbon crude together when the mixture is at the temperature of from about 100.degree. F. to about 200.degree. F. to form the pipeline-transportable oil-in-water emulsion(s), and is also one of the salient features of this invention. The objective of this device 108 is to coalesce most or all of the water present, including any water that might be present in the produced hydrocarbon crude as water-in-oil emulsion and/or as "free" water, into one continuous phase, and simultaneously disperse all the oil in the form of small droplets in this continuous water phase. Water, if any, present in the produced hydrocarbon crude in the form of water-in-oil emulsion and/or "free" water is converted, changed, or altered in the device 108 into oil-in-water emulsion(s). The degree of conversion or alteration sought is 100%. In order to avoid production of an inverted-phase emulsion (i.e. an oil continuous emulsion), the emulsion composition(s) is preferably initially passed through the device 108 in a relatively pure state (i.e. not combined or mixed with the produced hydrocarbon crude) before being combined or admixed with the produced hydrocarbon crude at the entrance of conduit 50 in order to wet the mixer internals of the device 108 with the desired water continuous phase. As will be discussed below in greater detail, the device 108 has various embodiments (as illustrated in FIGS. 4-14) and may be employed singly (see FIG. 3), or in parallel (see FIG. 2), to produce multimodal oil-in-water emulsion(s) having a lower viscosity than the viscosity of a unimodal oil-in-water emulsion(s). The static shearing and static mixing device 108 is preferably cylindrical with any suitable diameter, such as from about 0.2 inches to about 6.0 feet.

The effluent of the static shearing and static mixing device 108 is discharged into a conduit 110 and is substantially a water-external, oil-in-water emulsion(s) that is suitable for pipeline transportation. However, this oil-in-water emulsion(s) may contain extra water relative to that required to achieve a certain pipeline viscosity. A sampler 112 is provided within conduit 110 such that the oil-in-water emulsion(s) leaving the static shearing and static mixing device 108 passes through the sampler 112 whereby the quality of oil-in-water emulsion(s) achieved (including any water-in-oil emulsion(s) that might have been initially contained within the produced hydrocarbon crude and subsequently converted or changed in the static shearing and static mixing device 108 into the oil-in-water emulsion(s)) can be checked and determined. Conduit 110 also includes a valve 113 for regulating or terminating the flow of oil-in-water emulsion(s) therethrough.

If needed, and optionally, the formulated oil-in-water emulsion(s) can be recycled through a line 114, using a recycle pump 99, and back to the point of where the mixture of emulsifying composition(s) and produced hydrocarbon crude is introduced into the static shearing and static mixing device 108 to ensure formation of proper oil-in-water emulsion(s). To accomplish this recycle operation, recycle pump 99 is energized after valve 113 in conduit 110 is closed and a valve 115 (which is normally closed) in conduit 114 is opened. A temperature indicator 116 is provided in conduit 110 to monitor the temperature of the oil-in-water emulsion(s) flowing therethrough. Optionally, degassing boot 118 may also be provided in conduit 110 if degassing of the oil-in-water emulsion(s) is desired or needed. After the degassing boot 118, the pipeline-transportable oil-in-water emulsion(s) flows through a heat exchanger 120 and into an emulsion tank 122, or directly to a pipeline 123. The objective of the heat exchanger 120 is to provide an option for cooling the oil-in-water emulsion(s) flowing through conduit 110 to a temperature below about 120.degree. F., preferably below about 100.degree. F., more preferably from about 80.degree. F. to about 100.degree. F. Some oil-in-water emulsion(s) of this invention are temperature sensitive. At high temperatures (i.e. above about 120.degree. F.) these oil-in-water emulsion(s) may have reduced stability. In order to achieve a more stable oil-in-water emulsion(s), the temperature of the oil-in-water emulsion(s) flowing through the conduit 110 should be lowered below about 120.degree. F. At temperatures below about 120.degree. F., the stability of the oil-in-water emulsion(s) of this invention increases.

In the emulsion tank 122, the pipeline-transportable oil-in-water emulsion(s) is ready to be transmitted or transported through a conduit 124 to the pipeline 123. The quality of the oil-in-water emulsion(s) may be checked by another meter 126 having a cut monitor and sampler and, if satisfactory, it is sent to the pipeline 123 for transportation to a desired destination.

It should be noted that as long as the temperature of the oil-in-water emulsion(s) within the emulsion tank 122 is below about 120.degree. F., there should be no problems with the oil-in-water emulsion(s) with respect to stability. Similarly, as long as the quantity of water in the effluent oil-in-water emulsion(s) is greater than what is needed, there should be no problems with the oil-in-water emulsion(s) with respect to pipeline-viscosity standpoint, especially for Athabasca bitumen. Excess water in the oil-in-water emulsion(s) is of no major concern when the oil-in-water emulsion(s) is to be transported through a pipeline that is not too long, such as one (1) to two (2) miles. However, excess water for a long pipeline should not be too large because there may be limitations in the pipeline from a pumping-capacity standpoint. There could be a problem, especially when the produced hydrocarbon crude is Athabasca bitumen, if the amount of water in the effluent oil-in-water emulsion(s) is less than what is required from an effective pipeline-viscosity standpoint. Once the amount of water in the formulated oil-in-water emulsion(s) is the appropriate amount for an effective pipeline-viscosity, the formulated oil-in-water emulsion(s) may be pumped or transported through a pipeline of any length (such as over 1,000 miles) without any fears or concerns about the formulated oil-in-water emulsion(s) failing and/or breaking down into a mixture or phases that do not possess an effective viscosity for pipeline transportation. As was previously indicated, a salient feature of the oil-in-water emulsion(s) of this invention is that although the formulated oil-in-water emulsion may fail and/or break down in a pipeline into a mixture comprising an at least partially (i.e. partially or substantially) coalesced oil droplets in the water continuous phase and residual oil-in-water emulsion(s), the mixture has a viscosity that is less than or equal to the viscosity of the original oil-in-water emulsion(s) in spite of the fact that the coalesced oil droplet phase itself has a viscosity larger than the viscosity of the original oil-in-water emulsion(s). It should be understood that the mixture may include some (but not a substantial amount) formed oil-in-water emulsion that has inverted into a water-in-oil emulsion. Such water-in-oil emulsion may be part of the coalesced oil droplet phase and/or the residual oil-in-water emulsion and/or separate from both the coalesced oil droplet phase and the residual oil-in-water emulsion. With the emulsifier agent(s) of this invention in combination with other features of this invention, when the oil-in-water emulsion(s) fail or breakdown in a pipeline into the mixture comprising at least partially coalesced oil droplets and a residual oil-in-water emulsion(s), a substantial proportion of the original, formulated oil-in-water emulsion(s) is not inverted into a water-in-oil emulsion. The residual oil-in-water emulsion(s) may be defined as the remaining oil-in-water emulsion(s) from the original oil-in-water emulsion(s) whose contained dispersed oil droplets have not at least partially coalesced. These features of the present invention enable the mixture comprising the at least partially coalesced oil droplets and residual oil-in-water emulsion to be continuously pumped or otherwise transported through the same pipeline (i.e. pipeline 123) that the original oil-in-water emulsion(s) was introduced into, without the need for removing the mixture to reformulate the oil-in-water emulsion(s). However, one of the desirable qualities of the oil-in-water emulsion(s) of this invention is that if there is a breakdown or failure in the original oil-in-water emulsion(s) into the coalesced oil droplet-residual emulsion mixture, the original oil-in-water emulsion(s) may be easily reformulated by merely passing the mixture through another device 108 which may be situated within the pipeline that is transporting the oil-in-water emulsion(s) or off to the side of the pipeline in a bypass loop, as illustrated in FIG. 3. Thus, if desired, such reformulation may be easily accomplished even though it is not necessary to do so to continue the pumping or transportation of the failed or broken down original oil-in-water emulsion(s).

The emulsifying agent(s) of this invention used in the preparation of the oil-in-water emulsions may gradually become inactivated during pipeline flow, depending on the original concentration or quantity of emulsifying agent(s) employed, the temperature of the emulsion-forming constituents (i.e. crude and emulsifying composition) at formulation, etc. Regardless of any formulation condition, the formed oil-in-water emulsion will eventually separate into the two-phase mixture (i.e. the coalesced oil droplet-residual emulsion mixture) which, as was indicated above, will continue to flow under ordinary circumstances. The total distance through a pipeline in which an oil-in-water emulsion may be pumped or otherwise transported prior to separation into the two-phase mixture also depends on the original concentration or quantity of the emulsifying agent(s) employed, and the temperature of the emulsion forming constituents at formulation, as well as other properties of the hydrocarbon crude oil and aqueous phase (i.e. water, brine, or the like), and pipeline and pumping conditions. If, for any reason, the oil-in-water emulsion can not be prepared with sufficient stability to be pumped (or otherwise transported) over the total length of a pipeline, another embodiment of the present invention provides for remedial procedures to restore the oil-in-water emulsion in order to allow for the continued transportation of the formed oil-in-water emulsion through a pipeline for any desired distance. More specifically, it has been discovered that through the addition of additional aqueous phase and/or the addition of additional concentrated emulsifying composition [or additional pure emulsifying agent(s)] into the pipeline that has been transporting the original formed oil-in-water emulsion that has separated into the two-phase mixture (or the coalesced oil droplet-residual emulsion mixture), the separated oil-in-water emulsion can be restored into the original formed oil-in-water emulsion with sufficient agitation, such as by pumping or the like. The selection of additional aqueous phase and/or additional concentrated emulsifying composition [or pure emulsifying agent(s)] depends on the condition or state of the separated oil-in-water emulsion, the pipeline and pumping conditions, the desires of the pipeline operator and refiner or other receiver of the oil-in-water emulsion, and etc. Depending further on the pipeline and pumping conditions, it has been discovered that should even the original formed oil-in-water emulsion completely fail or otherwise transform into a highly viscous oil continuous system, such oil continuous system can be restored into the original formed oil-in-water emulsion through the addition or injection into the pipeline of additional emulsifying composition along with agitation, such as pumping or shearing and mixing statically. The use of this technique to correct a total oil-in-water emulsion failure would require that the necessary quantities of emulsifying composition be available and injection pumps be located at the location in the pipeline where the total failure has occurred.

The addition of additional aqueous phase into the pipeline transporting or carrying the separated oil-in-water emulsion allows the separated oil-in-water emulsion to be transported even if the separated emulsion should show a tendency to inversion or total failure into an oil continuous system. The amount of additional aqueous phase required depends on the properties of the crude, but is typically of an amount sufficient to increase or maintain the total aqueous phase concentration in a given volume of oil-in-aqueous phase emulsion in a range of from about 40% to about 60% (preferably 45% to 55%) volume percent. The utilization of the additional aqueous phase technique requires that the additional quantities of aqueous phase and injection pumps be available for use when and at the pipeline location where the originally formed oil-in-water emulsion separates into the emulsion mixture comprising the coalesced oil droplet phase and the residual oil-in-water emulsion phase. The amount of additional aqueous phase to be added must also be considered in relation to receiving tankage and treatment equipment at the pipeline termination.

The addition of additional concentrated emulsifying compositions [or additional pure emulsifying agent(s)] either alone or in combination with additional aqueous phase has some advantages over the employment of aqueous phase alone. A concentrated emulsifying composition may be defined as that amount of emulsifying composition that is necessary or equivalent for raising or maintaining the emulsifying agent(s) concentration of from about 250 ppm to 1500 ppm or higher of emulsifying agent(s) by weight of hydrocarbon oil/crude, after the emulsifying composition is added or injected into the separated oil-in-water emulsion. This procedure results in a lower emulsion mixture viscosity and a smaller increase in the total volume of the oil-in-water emulsion. Additional concentrated emulsifying composition [or additional pure emulsifying agent(s)] either alone or in combination with additional aqueous phase should be added or injected into the pipeline before or soon after separation and before any substantial portion of the aqueous phase is absorbed into the hydrocarbon oil/crude phase.

The additional concentrated emulsifying composition [or additional pure emulsifying agent(s)] either alone or in combination with additional aqueous phase may be used on a routine basis to reduce the total quantity of emulsifying agent(s) initially employed or required by having one or more intermediate emulsifier injection points along the pipeline transporting the oil-in-water emulsion in order to periodically inject the additional concentrated emulsifying composition [or additional pure emulsifying agent(s)], either alone or in combination with additional aqueous phase. If all of the required emulsifying agent(s) are employed initially at the beginning of the pipeline, excess emulsifying agent(s) is required to provide the necessary safety margin needed to ensure that separation or total failure does not occur. By the use of one or more intermediate emulsifier injection points along the pipeline transporting the oil-in-water emulsion, the total quantity of emulsifying agent(s) to be used can be optimized such that there is no excess or waste of emulsifying agent(s) at any point along the pipeline. Thus, the total quantity of emulsifying agent(s) used along the entire length of the pipeline would be less than the quantity of emulsifying agent(s) used for a sole injection only at the beginning of the pipeline.

It should also be pointed out that solid pellets of pure emulsifying agent(s) may be placed or injected periodically into the pipeline (either at the beginning or at intermediate positions) carrying or transporting oil-in-water emulsion in order to maintain the oil-in-water emulsion in an emulsion state while preventing separation or total failure. The solid pellets of pure emulsifying agent(s) injection procedure is thus another means of optimizing the quantity of emulsifying agent(s) used because the solid pellets would constantly, gradually emit, put forth, or dissolve fine solid quantities of pure emulsifying agent(s) into the stream of oil-in-water emulsion as the solid pellets travel through the pipeline along with the oil-in-water emulsion, allowing the initial quantity of emulsifying agent(s) used to form the oil-in-water emulsion to be smaller or less than the quantity that would have to be used if the solid pellets were not employed. Therefore, another embodiment of the present invention provides for a method for restoring the properties of a water continuous emulsion with a hydrocarbon crude after the emulsion has experienced phase separation in a pipeline comprising either or a combination of the following steps: (1) adding on a continuous basis at one or more points along the pipeline additional aqueous phase to the flowing separated emulsion to increase the total water concentration from 40% to 60% by volume; (2) adding on a continuous basis at one or more points along the pipeline additional emulsifying composition (or emulsifying agent(s) which may be in solid pellet or particulate form) to the flowing separated emulsion to increase the stability of the oil-in-water emulsion in order that it may be pumped to the end of the pipeline without total failure or inversion into an oil continuous phase. The present invention further provides for a method for reducing the total quantity of emulsifying agent(s) necessary for pipeline transportation of a heavy crude or bitumen water continuous emulsion and simultaneously reducing the risk of emulsion separation comprising the following steps: (1) preparing an oil-in-water emulsion with a smaller quantity of emulsifying agent(s) necessary for transporting the formed oil-in-water emulsion over the entire length of the pipeline; (2) injecting at one or more points along the pipeline additional emulsifying compositions (or emulsifying agent(s) which may be in solid pellet or particulate form) in order to minimize and optimize the total quantity of emulsifying agent(s) required. The solid form of the emulsifying agent(s) may be placed in the formed oil-in-water emulsion at the beginning of the pipeline to flow with the flowing emulsion to gradually dispose of additional emulsifying agent(s) in the emulsion while flowing through the length of the pipeline.

After the oil-in-water emulsion(s) has been transported or pumped through the pipeline 123 to its final destination, the oil droplets are separated from the oil-in-water emulsion(s) in a separating station 300 that is positioned at the end of the pipeline 123. The separated oil leaves the separating station through pipeline 302 and the residual water product after the oil has been separated, which is water plus any additives (e.g. ethylene glycol, etc.), should be recycled back to the water tank 26, or the tank 58, through conduit 304 in order to be admixed with the produced hydrocarbon crude. Separating the oil droplets from the oil-in-water emulsion(s) may be accomplished by any suitable means, such as heating the oil-in-water emulsion(s) above the phase inversion temperature (P.I.T.), which is generally from about 180 F. to about 210 F., and/or adding deemulsifier(s). Any deemulsifier(s) added to the oil-in-water emulsion(s) and contained within the residual water product after the oil has been separated has little or no effect on the emulsifying agent(s) of this invention.

In another embodiment of the present invention, the formed oil-in-water emulsion is broken, destroyed, dissipated, or any of the like (hereinafter referred to as "breaking the oil-in-water emulsion") in order to recover the oil phase while simultaneously destroying any undesirable components resulting from degradation and/or reduction of the emulsifying agent (s) while in transit. Such undesirable components as phenols and other phenolic structure compounds may result from the emulsifying agent(s) of this invention degrading or being reduced while the formed oil-in-water emulsion is being transported through the pipeline. Thus, it becomes desirable to remove these undesirable components which are generally water soluble. It becomes even more desirable to remove these undesirable components while simultaneously breaking the formed oil-in-water emulsion. In the present invention, such undesirable phenol components are removed while simultaneously breaking the formed oil-in-water emulsion through the use of potassium permanganate, preferably employed in a quantity or concentration of from about 500 ppm to about 15,000 ppm (more preferably 1000 to 2000 ppm) of potassium permanganate by weight of oil-in-water emulsion. Potassium permanganate breaks up the formed water continuous emulsion and simultaneously destroys any undesirable phenols in a single-step operation.

Potassium permanganate is a powerful oxidizing chemical which destroys phenolic compounds and other undesirable compounds containing benzene by attacking the double bonds. Potassium permanganate also reacts and/or breaks the ##STR3## repeat segments or units in the emulsifying agent(s) to break the water continuous emulsion. During the attack and/or reaction, water and manganese dioxide and carbon dioxide form, along with byproducts. When potassium permanganate is utilized in removing phenol in a holding tank, the phenol is oxidized rapidly at a pH of 7.0 to 11.0, preferably 8.5 to 9.5. A retention time of from fifteen minutes to about six hours in a reactor and/or a retention time of fifteen minutes to two weeks in a tankage, is sufficient to insure complete oxidation of the phenol. The initial reaction takes place almost immediately, and almost 90% of the phenol is generally oxidized in the first ten minutes. Other suitable oxidizers for phenol treatment and breaking the water continuous emulsions are ozone (O.sub.3), hydrogen peroxide (H.sub.2 O.sub.2), and chlorine (Cl.sub.2). These oxidizers are typically employed in any suitable manner (e.g. chlorination, ozonation, etc.) in quantities ranging from 500 ppm to 15,000 ppm of oxidizer by weight of oil-in-water emulsion.

A preferred procedure for treating the oil-in-water emulsion with potassium permanganate is to mix (either statically or dynamically and/or in a reactor) the water continuous emulsion with a diluted stream of potassium permanganate (i.e. a potassium permanganate-aqueous mixture having 85 wt. % to 99 wt. % of the aqueous phase). The potassium permanganate preferentially reacts with the emulsifying agent(s) as opposed to constituents in the hydrocarbon oil/crude. After thorough mixing, the mixture is preferably discharged into a conventional vessel for a quiescent period ranging from about fifteen minutes to about two weeks. Typically, during the quiescent period, the hydrocarbon oil/crude coagulates and rises to the top while the aqueous phase settles to the bottom. The hydrocarbon oil/crude is removed off of the aqueous phase as effluent and is fed into a desalter where separation of the mixture occurs into Waste Water and hydrocarbon oil/crude for refining purposes. The waste water may have to be further treated with an oxidizer (e.g. dilute KMnO.sub.4, ozone, chlorine, etc.) and a mixer (e.g. static mixer, high shear pump, etc.) in accordance with the procedure as previously set forth for treating water continuous emulsions for phenols while simultaneously breaking the emulsion.

Alternatively to separating the oil droplets from the oil-in-water emulsion(s) or breaking the oil-in-water emulsions, the existing oil-in-water emulsion(s) can be used in its existing state, such as for fuel, and there would be no need to separate the oil droplets from the existing oil-in-water emulsion. Thus, in those instances where the oil-in-water emulsion(s) is to be burned as fuel, the oil-in-water emulsion(s) can be fed directly to a boiler (e.g. utility boiler, fluidized bed boiler, etc.). No separation step would have to be employed unless the BTU content of the oil-in-water emulsion(s) is too low.

The emulsifying agent(s) of this invention may be any emulsifying agent which, when combined with an appropriate amount of water, is capable of forming in the produced hydrocarbon crude an oil-in-water emulsion when the temperature of the crude-emulsifying agent mixture is from about 100.degree. F. to about 200.degree. F. Generally, unless a broad-based emulsifying agent is used, a mixture of at least two emulsifying agents is employed. Surface-active agents used to form oil-in-water emulsion(s) may be anionic, cationic, nonionic, amphoteric, and the like. A desired and preferred characteristic is a high degree of oil insolubility. Preferably, the surface active agents are substantially insoluble in oil. Most of the inexpensive and efficient candidates for forming crude oil-in-water emulsion(s) are either anionic or nonionic. Nonionics are presently preferred because they are generally cheaper and not affected by the salinity of the water.

The best known of all the anionic-active emulsifying agents are the soaps which are the salts of the long-chain fatty acids, derived from naturally occurring fats and oils, in which the acids are found as triglycerides. The soaps used as emulsifying agents may be obtained from natural oils, in which case they will consist of a mixture of fatty acids, the precise nature of the mixture depending on the fat or oil employed. The mixed fatty acids of tallow, coconut oil, palm oil, and the like, are those commonly employed. The acids derived from tallow, for instance, may be partially separated by filtration or by pressing into "red oil" (principally oleic acid) and the so-called "stearic acid" of commerce, which is sold as single-, double-, or triple-pressed, depending on the extent to which oleic acid is separated. Such stearic acid is actually a mixture of stearic and palmitic acids.

The nonionic emulsifying agents can be classified into five types, namely, ether linkage, ester linkage, amide linkage, miscellaneous linkages, and multiple linkage. Preferred nonionic emulsifying agent(s) are substantially oil insoluble and are those selected from the compounds having the general formula: ##STR4## where each of R, R.sub.1 and R.sub.2 is any hydrocarbon group, preferably an alkyl radical containing from about 8 to about 21 carbon atoms, and each of y and y.sub.1 is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve. Preferably, each of y and y.sub.1 ranges from about 4 to about 100, more preferably from about 30 to about 100. Most preferably, each of R, R.sub.1, and R.sub.2 is C.sub.9 H.sub.19, and each of y and y.sub.1 is 40 or 100. When the oil-in-water emulsion(s) of this invention are formulated with the nonionic emulsifying agent(s) represented by the general formula (1) and/or the general formula (2), the static shearing and static mixing device 108 is preferably employed without being preceded or followed by any dynamic shearing and mixing device, because it has been discovered that the longevity quality of the formulated oil-in-water emulsion(s) is affected if produced through the use of a dynamic shearing and/or mixing device. However, even if nonionic emulsifying agent(s) represented by the general formula (1) and/or the general formula (2) is employed along with dynamic shearing and/or dynamic mixing, and the formulated oil-in-water emulsion(s) fails and/or breaksdown while being transported through a pipeline, it has been discovered that the viscosity of the failed and/or brokendown mixture, which comprises coalesced and separated oil droplets in the water continuous phase and residual oil-in-water emulsion, is less than or equal to the original formulated oil-in-water emulsion(s). It has been discovered that this is true even though the viscosity of coalesced and separated oil droplets is more than the original formulated oil-in-water emulsion(s). Thus, the failed and/or brokendown mixture may be continually pumped through the pipeline without any concerns for non-effective pipeline-viscosity.

Other preferred nonionic emulsifying agent(s), especially when the produced hydrocarbon crude is Athabasca bitumen, are those selected from the compounds which are substantially oil insoluble and have the general formula: ##STR5## where n is from about 7 to about 20, preferably 11, and y is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the means of a normal Gaussian distribution curve and is from about 101 to about 250, preferably from about 120 to about 180, more preferably about 150; and ##STR6## wherein n.sub.1 is from about 7 to about 18, preferably about 8, n.sub.2 is from about 7 to about 18, preferably about 8, and y.sub.1 is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 101 to about 250, preferably from about 120 to 180, more preferably about 150.

Preferably, the nonionic emulsifying agent(s) of this invention is a combination of the compounds having the general formula (3) and the compounds having general formula (4), with the compounds having the general formula (4) being at least 40% by weight of the combination. More preferably, the compounds having general formula (4) are from about 50% by wt. to about 85% by wt. of the combination.

The most prominent members of the class of nonionic emulsifying agent(s) represented by the foregoing general formulas (1), (2), (3) and (4) are those compounds formed by the reaction of a hydrophobic hydroxyl-containing compound, e.g., an alcohol or phenol, with ethylene oxide. The ethylene oxide groups, for example, may be added to any desired extent.

The emulsifying composition(s) of this invention can comprise emulsifying agent(s) represented by the general formula (1) and/or the general formula (2) in combination with the emulsifying agent(s) represented by the general formula (3) and/or the general formula (4). Typically, when such combination or combinations are employed, the amount or quantity of emulsifying agent(s) represented by the general formula (3) and/or the general formula (4) would comprise from about 20% by wt. to about 80% by wt. of the total amount or quantity of the emulsifying agent(s) employed within the emulsifying composition(s).

It has been discovered that when the oil-in-water emulsion(s) of this invention are produced or formulated with the nonionic emulsifying agent(s) represented by the general formula (3) and/or the general formula (4), any form or means of agitation may be utilized for such production or formulation. Any dynamic shearer or mixer may be utilized, as well as the preferred static shearing and static mixing device 108.

Should a portion of the oil droplets in the oil-in-water emulsion(s) formulated with the nonionic emulsifying agent(s) represented by any of the general formulas (1)-(4), either taken singly or in combination, partially coalesce for any reason to form partially coalesced oil, the mixture comprising the oil-in-water emulsion including the partially coalesced oil may be continually transported or pumped through a pipeline for the same reasons that have been previously stated. To reiterate and to be more specific, the viscosity of the oil-in-water emulsion containing partially coalesced oil has a viscosity lower than or equal to the original oil-in-water emulsion(s) in spite of the fact that the viscosity of the partially coalesced oil droplets is larger than the viscosity of the originally formulated oil-in-water emulsion(s). Thus, the failed and/or brokendown mixture may even have a viscosity that makes it more favorable for pipeline transportation than the originally formulated oil-in-water emulsion(s).

The presently nonionic emulsifying agent(s) having an ester linkage include compounds of the following general formula: ##STR7## where R is any hydrocarbon group, preferably an alkyl radical containing from about 8 to about 21 carbon atoms, more preferably R is C.sub.9 H.sub.19 ; and y is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 4 to about 250, preferably from about 40 to 150, more preferably 40 or 100; and are substantially oil insoluble as defined above.

The esters formed by the reaction of the fatty acids with polyhydric alcohols are a particularly interesting group of nonionic emulsifiers, in that, depending on the nature of the alcohol used, they may be predominantly hydrophilic and are especially suitable as oil-in-water emulsifiers.

An example of an ester-linkage surfactant which is a good emulsifying agent is: ##STR8##

Nonionic emulsifying agent(s) with amide linkages are compounds of the general formula: ##STR9## where R is any hydrocarbon group, preferably an alkyl radical containing from about 8 to about 21 carbon atoms, more preferably R is C.sub.9 H.sub.19 ; and each of y.sub.1 and y.sub.2 is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 4 to about 250, preferably from about 40 to 150, more preferably 40 or 100; and are substantially oil insoluble as defined above.

Another nonionic emulsifying agent(s) that has been found to be suitable in the process of this invention is polyethoxylated alcohol(s) having the general formula: ##STR10## wherein R is an alkyl having from about 7 to about 20 carbon atoms and y is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 4 to about 250. More preferably, R is an alkyl having from about 12 to about 18 carbon atoms and y is from about 120 to about 180.

In a more preferred embodiment of the present invention, the emulsifying agent(s) is or are those emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 1966 to about 9188, and the general formula: ##STR11## wherein n.sub.1 is an integer and has a value of from about 7 to about 20, preferably 11, and y.sub.1 is an integer having a value of from about 4 to about 1000; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188. The emulsifying agent(s) has at least one ethoxylated alkylphenol compound having the general formula: ##STR12## wherein n.sub.1 has a value of from about 7 to about 20, preferably 11; and y.sub.1 is greater than 100, preferably greater than 100 but less than 1000, and the ethoxylated alkylphenol compound of general formula (5A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s).

More preferably, the dispersity of the molecular weight distribution of the emulsifying agent(s) represented by general formula (5) is from about 1.0 to about 2.5, most preferably about 1.0 to 2.0. The weight average molecular weight of the emulsifying agent(s) is more preferably from about 3726 to about 6548, most preferably from about 4606 to 5668. More preferably, at least about 70% by weight (most preferably, at least about 85% by weight) of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188.

The emulsifying agent(s) in the present invention may also be those emulsifying agent(s) selected from the ethoxylated dialkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 2519 to about 11,627, and the general formula: ##STR13## wherein n.sub.1 is an integer and has a value of from about 7 to about 18, n.sub.2 is an integer and has a value of from about 7 to about 18, and y.sub.2 is an integer having a value of from about 4 to about 1,000; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627. The emulsifying agent(s) has at least one ethoxylated dialkylphenol compound having the general formula: ##STR14## wherein n.sub.1 has a value of from about 7 to about 18, n.sub.2 has a value of from about 7 to about 18, and y.sub.2 is greater than 100, preferably greater than 100 but less than 1000; and the ethoxylated dialkylphenol compound of general formula (6A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s).

More preferably, the dispersity of the molecular weight distribution of the emulsifying agent(s) represented by the general formula (6) is from about 1.0 to about 2.5, most preferably from about 1.0 to 2.0. The weight average molecular weight of the emulsifying agent(s) is more preferably from about 4714 to about 8547, most preferably from about 6039 to about 7227. More preferably, at least about 70% by weight (most preferably, at least about 85% by weight) of the emulsifying agent(s) comprises the ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627.

The emulsifying agent(s) may be a combination of the ethoxylated alkylphenol compounds having the general formula (5) and the ethoxylated dialkylphenol compounds having the general formula (6) in any percent by weight proportion provided that the dispersity of the molecular weight distribution of the entire combination is from about 1.0 to about 5.0 (more preferably about 1.0 to about 2.5 and most preferably about 1.0 to 2.0), and the weight average molecular weight in the combination of the emulsifying agent(s) [or in general formula (5) and/or in general formula (6)] is about 1966 to about 11,627 (more preferably about 3726 to about 8547, most preferably about 4606 to about 7227). Furthermore, the entire combination should comprise at least 50% by weight (more preferably at least about 70% by weight, most preferably at least about 85% by weight) of the ethoxylated alkylphenol compound and the ethoxylated dialkylphenol compound wherein the ethoxylated alkylphenol compound has a molecular weight of from about 1966 to about 9188 and the ethoxylated dialkylphenol compound has a molecular weight of from about 2519 to about 11,627. More preferably, the compounds having the general formula (5) are from about 30% by weight to about 80% by weight of the combination. Furthermore, at least 1% by weight (preferably 1% to 90% by weight) of the combination of the ethoxylated alkylphenol compound having the general formula (5) and the ethoxylated dialkylphenol compound having the general formula (6) comprises the ethoxylated alkylphenol compound having the general formula (5A) and/or the ethoxylated dialkylphenol compound having the general formula (6A), where y.sub.1 and y.sub.2 are both greater than 100, preferably greater than 100 but less than 1000.

Dispersity of the molecular weight distribution of the polymeric emulsifying agent(s) is defined as the ratio of the weight-average molecular weight (M.sub.w) of the emulsifying agent(s) to the number-average molecular weight (M.sub.n) of the emulsifying agent(s), or M.sub.w /M.sub.n. M.sub.n is biased toward the lower molecular weight fractions in the polymeric emulsifying agent(s) while M.sub.w is biased toward the higher molecular weight fractions. Dispersity depends on the breadth of the molecular weight distribution for the polymeric emulsifying agent(s) and measures the polydispersity in the polymeric emulsifying agent(s).

The weight-average molecular weight M.sub.w is obtained from conducting light scattering measurements on the emulsifying agent(s) and is defined as

where w.sub.x is the weight-fraction of molecules whose weight is M.sub.x. M.sub.x can also be defined as ##EQU1## where C.sub.x is the weight concentration of M.sub.x molecules, C is the total weight concentration of all the polymeric emulsifying agent(s) molecules, N.sub.x is the number of moles whose weight is M.sub.x, and the following relationships hold: ##EQU2##

The number-average molecular weight M.sub.n is determined by the measurement of colligative properties such as freezing point depression (cryoscopy), boiling point elevation (ebulliometry), osmotic pressure, and vapor pressure lowering. M.sub.n is defined as the total weight w of all the molecules in the polymeric emulsifying agent(s) divided by the total number of moles present. Stated alternatively, the number-average molecular weight is defined by: ##EQU3## where the summations are from 1 to the number of different sizes of polymer molecules in the emulsifying agent(s), and N.sub.x is the number of moles whose weight is M.sub.x.

For a comprehensive discussion of dispersity,M.sub.w, and M.sub.n, and other macromolecular science properties, such as the physical and organic chemistry of the reactions by which polymer molecules are synthesized, see the following publications: Principles of Polymerization by Odian (copyright and published in 1970 by McGraw-Hill Inc.); Introduction to Polymer Science and Technology: An SPE Textbook by Kaufman et al. (copyright and published in 1977 by John Wiley & Sons Inc.); Principles of Polymer Chemistry by Flory (copyright and published in 1953 by Cornell University); and Macromolecules by Elias (Volume 1 and 2; copyright in 1977 by Plenum Press, New York, and published in 1977 by John Wiley & Sons, Ltd.). All of these publications are incorporated entirely herein by reference thereto.

As will be more thoroughly discussed hereinafter in the Examples for the more preferred emulsifying agent(s) represented by the general formulas (5) and/or (6), the shear life (the measure of the stability of an emulsion) of formed oil-in-water emulsions utilizing the more preferred emulsifying agent(s) are commercially acceptable (i.e. equal an emulsion shear stability to or greater than 40 mins.) provided that the following parameters are conformed to or are followed:

(1) the dispersity of the molecular weight distribution for the emulsifying agent(s) is from about 1.0 to about 5.0 (more preferably 1.0-2.5, most preferably 1.0-2.0);

(2) the weight average molecular weight of the emulsifying agent(s) has a value of from about 1966 to about 11,627 (more preferably from about 3726 to about 8547, most preferably from about 4606 to about 7227), depending on which of the emulsifying agent(s) are employed, those represented by the general formula (5) and/or those represented by the general formula (6); and

(3) that at least 50% by weight (more preferably at least about 70% by weight, most preferably at least about 85% by weight) of the emulsifying agent comprises the ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188 and/or the ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627.

In another more preferred embodiment of the present invention, especially when the oil-in-water emulsion(s) are to be subterraneously formed in a short period of time (e.g. 0.10 to 20 secs.), the emulsifying agent(s) is or are those emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 558 to about 2504, and the general formula: ##STR15## wherein n.sub.1 is an integer and has value of from about 7 to about 14, preferably 8, and y.sub.1 is an integer having a value of from about 4 to about 200; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 558 to about 2504. The emulsifying agent(s) has at least one ethoxylated alkylphenol compound having the general formula: ##STR16## wherein n.sub.1 has a value of from about 7 to about 14, preferably 8; and y.sub.1 is greater than 100, preferably greater than 100 but less than 200, and the ethoxylated alkylphenol compound of general formula (7A) preferably comprises at least about 1% by weight (more preferably from about 1% to about 10% by weight) of the emulsifying agent(s).

More preferably, the dispersity of the molecular weight distribution of the emulsifying agent(s) represented by general formula (7) is from about 1.0 to about 3.0, most preferably about 1.0 to 2.0. The weight average molecular weight of the emulsifying agent(s) is more preferably from about 646 to about 1844, most preferably from about 866 to 1404. More preferably, at least about 70% by weight (most preferably, at least about 85% by weight) of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 558 to about 2504.

The emulsifying agent(s) may be a combination of the ethoxylated alkylphenol compounds having the general formula (7) and emulsifying agent(s) selected from the ethoxylated alkyl compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 2458 to about 4218, and the general formula: ##STR17## wherein n.sub.1 is an integer and has a value of from about 9 to about 14, preferably 11, and y.sub.1 is an integer having a value of from about 4 to about 300; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 2458 to about 4218. The emulsifying agent(s) represented by general formula (8) has at least one ethoxylated alkylphenol compound having the general formula: ##STR18## wherein n.sub.1 has a value of from about 9 to about 14, preferably 11; and y.sub.1 is greater than 100, preferably greater than 100 but less than 300, and the ethoxylated alkylphenol compound of general formula (8A) preferably comprises at least about 1% by weight (more preferably from about 1% to about 75% by weight) of the emulsifying agent(s).

More preferably, the dispersity of the molecular weight distribution of the emulsifying agent(s) represented by general formula (8) is from about 1.0 to about 3.0, most preferably about 1.0 to 2.0. The weight average molecular weight of this emulsifying agent(s) is more preferably from about 2898 to about 3778, most preferably from about 3118 to 3558. More preferably, at least about 70% by weight (most preferably, at least about 85% by weight) of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound represented by general formula (8) having a molecular weight of from about 2458 to about 4218.

The ethoxylated alkylphenol compounds having the general formula (7) and the ethoxylated alkylphenol compounds having the general formula (8) are preferably combined or mixed in a percent by weight proportion such that the ethoxylated alkylphenol compounds having the general formula (7) preferably comprise from about 60% by weight to about 85% by weight of the combination or mixture, and the ethoxylated alkylphenol compounds having the general formula (8) preferably comprise from about 15% by weight to about 40% by weight of the combination or mixture. More preferably, the combination or mixture of the ethoxylated alkylphenol compounds having the general formula (7) and the ethoxylated alkylphenol compounds having the general formula (8) comprises from about 70% by weight to about 80% by weight of the ethoxylated alkylphenol compounds having the general formula (7) and from about 20% by weight to about 30% by weight of the ethoxylated alkylphenol compounds having the general formula (8).

The emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having the general formula (7) are particularly valuable in subterraneously forming (i.e., "down hole") oil-in-water emulsions in a commercially acceptable period of time and having a commercially acceptable shear life. A commercially acceptable period of time may be defined as that period of time ranging from about 0.10 secs. to about 20 secs. A commercially acceptable shear life has been defined as an emulsion shear stability equal to or greater than 40 mins. For down hole purposes it is desired that oil-in-water emulsion(s) be formed quickly and with a commercially acceptable shear life so that the high viscosity hydrocarbon being produced can be readily transported to the surface of the earth without the high viscosity hydrocarbon plugging the well tubing and/or retarding the transportation of the produced high viscosity hydrocarbon, and/or otherwise curtailing the production of the high viscosity hydrocarbon. Should the well tubing become plugged such as from failure of the oil-in-water emulsion because of a commercially unacceptable shear life, it may be necessary to pull the well tubing to unplug or replace well tubing.

Subterranean oil-in-water emulsions are formed with the emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having the general formula (7) by agitating (e.g. dynamically and/or statically) the produced hydrocarbon with an emulsifying composition at a temperature of from about 35.degree. F. to about 170.degree. F. and wherein the emulsifying composition comprises an aqueous phase and a minor amount of the emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having the general formula (7). The agitating comprises mixing below the surface of the earth and in proximity to the producing hydrocarbon formation the produced hydrocarbon with the emulsifying composition for a period of time ranging from about 0.10 sec. to about 20 secs., and preferably in a shear field with an intensity ranging from about 50 sec..sup.-1 to about 10,000 sec..sup.-1 (preferably 50 sec..sup.-1 to 5,000 sec..sup.-1). The emulsifying agent(s) selected from the ethoxylated alkylphenol compounds represented by the general formula (7) cause excellent oil-in-water emulsion(s) to be formed with a commercially acceptable shear life and within 0.10 to 20 secs. when mixed with an aqueous phase and a produced hydrocarbon at a temperature of from about 35.degree. F. to about 170.degree. F.

As will be more thoroughly discussed hereinafter in the Examples for the other more preferred emulsifying agent(s) represented by the general formula (7), the time to form quality oil-in-water emulsions utilizing the other more preferred emulsifying agent(s) represented by the general formula (7) is commercially acceptable (i.e., if formed within 0.10 to 20 secs.) provided that the following parameters are conformed to or are followed:

(1) the dispersity of the molecular weight distribution for the emulsifying agent(s) is from about 1.0 to about 5.0 (more preferably 1.0-3.0, most preferably 1.0-2.0);

(2) the weight average molecular weight of the emulsifying agent(s) has a value of from about 558 to about 2504 (more preferably from about 646 to about 1844, most preferably from about 866 to about 1404);

(3) that at least 50% by weight (more preferably at least about 70% by weight, most preferably at least about 85% by weight) of the emulsifying agent comprises the ethoxylated alkylphenol compound having a molecular weight of from about 558 to about 2504; and

(4) the temperature of the emulsifying composition (and hydrocarbon) is from about 35.degree. F. to about 170.degree. F.

It has been discovered that if the temperature of the emulsifying composition, or hydrocarbon plus emulsifying composition, including those emulsifying agent(s) selected from the ethoxylated alkylphenol compounds represented by general formula (7), is above about 170.degree. F., oil-in-water emulsion(s) do not form, unless the emulsifying agent(s) selected from the ethoxylated alkylphenol compounds represented by general formula (7) are admixed with or otherwise combined with emulsifying agent(s) selected from those ethoxylated alkylphenol compounds having general formula (8). As was previously mentioned, the combination or admixture of the ethoxylated alkylphenol compounds having the general formula (7) and the ethoxylated alkylphenol compounds having the general formula (8) comprises from about 60% by weight to about 85% by weight (more preferably 70% to 80% by weight) of the ethoxylated alkylphenol compounds having the general formula (7), and from about 15% by weight to about 40% by weight (more preferably 20% to 30% by weight) of the ethoxylated alkylphenol compounds having the general formula (8). By the admixing or the otherwise combining of the ethoxylated alkylphenol compounds having general formula (7) with the ethoxylated alkylphenol compounds having general formula (8), the temperature of the emulsifying composition (or the emulsifying composition plus hydrocarbon) may be as high as the boiling point temperature of the emulsifying composition (or the emulsifying composition plus hydrocarbon) which typically is about 212.degree. F., depending on the subterranean pressure, the exact constituency (and the mixing proportion of the various constituencies) of the emulsifying composition and the hydrocarbon, etc.

As will be more thoroughly discussed hereinafter in the examples for the other more preferred emulsifying agents comprising the mixture or combination of the emulsifying agent(s) represented by the general formula (7) and the general formula (8), the time to form quality oil-in-water emulsions utilizing the mixture or combination of the emulsifying agent(s) represented by the general formula (7) and/or with the emulsifying agent(s) represented by the general formula (8) is commercially acceptable (i.e., if formed within 0.10 to 20 secs.) provided that the following parameters are conformed to or are followed:

(1) the dispersity of the molecular weight distribution for the emulsifying agent(s) represented by general formula (7) is from about 1.0 to about 5.0 (more preferably 1.0-3.0, most preferably 1.0-2.0);

(2) the weight average molecular weight of the emulsifying agent(s) represented by general formula (7) has a value of from about 55s to about 2504 (more preferably from about 646 to about 1844, most preferably from about 866 to about 1404);

(3) that at least 50% by weight (more preferably at least about 70% by weight, most preferably at least about 85% by weight) of the emulsifying agent comprises the ethoxylated alkylphenol compound represented by general formula (7) having a molecular weight of from about 558 to about 2504; and

(4) the dispersity of the molecular weight distribution for the emulsifying agent(s) represented by general formula (8) is from about 1.0 to about 5.0 (more preferably 1.0-3.0, most preferably 1.0-2.0);

(5) the weight average molecular weight of the emulsifying agent(s) represented by general formula (8) has a value of from about 2458 to about 4218 (more preferably from about 2898 to about 3778, most preferably from about 3118 to about 3558);

(6) that at least 50% by weight (more preferably at least about 70% by weight, most preferably at least about 85% by weight) of the emulsifying agent comprises the ethoxylated alkylphenol compound represented by general formula (8) having a molecular weight of from about 2458 to about 4218;

(7) n.sub.1 in general formula (8) is from about 9 to about 14, as if n.sub.1 is below 9 or above 14, it has been discovered that oil-in-water emulsions of commercial acceptability do not generally form; and

(8) from about 60% by weight to about 85% by weight of the mixture or combination is the emulsifying agent(s) represented by general formula (7), and if less than 60% by weight or greater than 85% by weight of the emulsifying agent(s) represented by general formula (7) is employed, it has been discovered that oil-in-water emulsions of commercial acceptability do not generally form.

The emulsifying agent(s) used in the practice of the invention must enable formation of the oil-in-water emulsion(s) at elevated temperatures and retention of stability at ambient temperatures. Unless broad-based for such functionality, a mixture of two or more emulsifiers is employed, and is particularly preferred.

In yet another more preferred embodiment of the present invention, the emulsifying composition(s) comprising the aqueous medium, the ethoxylated alkylphenol compounds having the general formula (7) and the ethoxylated alkylphenol compounds having the general formula (8), in any suitable percent by weight proportion such as any of the previously mentioned percent by weight proportions, are injected directly through a well/wellbore into a subterranean hydrocarbon-bearing reservoir or formations having a hydrocarbon. When the emulsifying composition(s) for this embodiment of the present invention contacts the hydrocarbon at a temperature below about the phase inversion temperature (P.I.T.) for the oil-in-aqueous phase emulsion to be produced, an oil-in-aqueous phase emulsion is formed within the subterranean hydrocarbon-bearing reservoir. Typically, the emulsifying composition(s) contacts and mixes with at least a portion of the hydrocarbon (and connate water) in situ below about the P.I.T. to form or produce the oil-in-aqueous phase emulsion within the subterranean hydrocarbon-bearing reservoir, leaving a residual quantity of the hydrocarbon therein that did not formulate an oil-in-aqueous phase emulsion with the emulsifying composition(s). As was previously mentioned, the P.I.T. for the formed oil-in-aqueous phase emulsion is generally between about 180.degree. F. to about 210.degree. F., depending on the exact consistency of the oil-in-aqueous phase emulsion and the particular percent by weight proportions in which the constituents are combined. Preferably, after a known quantity of the emulsifying composition(s) is injected through the well/wellbore and into the hydrocarbon-bearing formation or reservoir, steam and/or hot water (i.e., water with a temperature of 150.degree. F. to 250.degree. F., depending on the pressure) is subsequently injected into the same hydrocarbon-bearing reservoir to follow the emulsifying composition(s). The steam and/or hot water accomplishes the dual objectives of thermally stimulating the formation by heating the same to raise the temperature and lower the viscosity of in situ hydrocarbon which facilitates oil-in-aqueous phase emulsion formation, while simultaneously pushing or driving the emulsifying composition(s) away from the wellbore and into the formation for contact, mixing and interacting with in situ hydrocarbons that are not in close proximity to the wellbore. Subsequently, the steam and/or hot water injection is terminated after the emulsifying composition has been sufficiently dispersed into and throughout the reservoir, followed by a shut-in of the well/wellbore, allowing the reservoir to soak for a sufficient period of time (e.g. one to ten days) to maximize and/or optimize the formulation of oil-in-aqueous phase emulsion. After the soak period, the well/wellbore is reopened, and oil-in-aqueous phase emulsion can be recovered by any suitable means for producing or recovering, such as with any of the pumps described in Chapter 11 entitled "Facilities, Operational Problems, and Surveillance" in the book Thermal Recovery by Michael Prats copyrighted 1982 by American Institute of Mining Metallurgical and Petroleum Engineers, published by Society of Petroleum Engineers (Henry L. Doherty, Memorial Fund of AIME). The entire process may be repeated to remove residual hydrocarbon and/or oil-in-aqueous phase emulsion remaining within the reservoir or formation and not having been recovered.

The emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8) are thermally stable up to a temperature of about 600.degree. F. or slightly higher, and are generally not adsorbed by the sands and clays of reservoir formations. The emulsifying composition(s) forms a low-viscosity aqueous phase continuous emulsion with improved mobility in the subterranean reservoir, and causes the reduction of residual oil saturation with increased ultimate recovery of the original reservoir hydrocarbons. Furthermore, concomitant with recovering the viscosity of in situ hydrocarbons, there is increased or accelerated hydrocarbon production with a corresponding reduction in thermal losses. Production period can be extended for those wells having a bottom hole temperature less than the usual 90.degree. to 100.degree. C. range, resulting in a reduction in the steam (and/or hot water)/oil ratio. Furthermore still, by employing the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8) for producing hydrocarbons from subterranean formations, the emulsifying composition(s) can be used for mobility control in steamflood or waterflood operations, and for improved sweep efficiency as a result of emulsion formation or injections into the high permeability zones to prevent channeling.

In a preferred embodiment of the present invention, a coemulsifying composition is injected directly through the well/wellbore into the hydrocarbon-bearing reservoir prior to or before the injection of the emulsifying composition(s) comprising the ethoxylated alkylphenol compounds having the general formula (7) and the general formula (8). The coemulsifying composition may be any suitable coemulsifying composition (e.g. anionic and/or nonionic) that can initially be adsorbed on the reservoir rock or formation such as to insure no adsorption of the emulsifying composition(s) comprising the ethoxylated alkylphenol compounds having the general formulas (7) and (8) as the same is being injected. While, as was previously indicated, the emulsifying composition(s) does not generally adsorb on sands and clays, in order to insure such nonadsorption, the coemulsifying composition(s) is employed for ultimate preventative purposes. Preferably, the coemulsifying composition(s) comprises an aqueous phase and a coemulsifying agent(s) selected from alkylarylsulfonates, lignosulfonates, and mixtures thereof. Lignosulfonates (or lignin sulfonates) are metallic sulfonate salts made from lignin of sulfite pulpmill liquors and have molecular weights ranging from about 1000 to about 20,000. More particularly, lignosulfonates are by-products of the sulfite process for separating cellulose pulp from wood and are formed by the reaction of SO.sub.2 and Ca(HSO.sub.3).sub.2 with wood which is typically a mixture composed of 67 to 80% holocellulose and 17 to 30% lignin, together with low percentages of resins, sugars, a variable amount of water, and potassium compounds. Lignosulfonates do not possess a well-characterized chemical structure, but are polyanionic natural polymers. The alkylarylsulfonates preferably possess the general formula RC.sub.6 H.sub.4 SO.sub.3 M wherein R is an alkyl having from 7 to 15 carbon atoms and M is an alkali metal (i.e., lithium, sodium, potassium, rubidium, cesium or francium), hydrogen, or ammonium or triethanolammonium or isopropylammonium. The coemulsifying composition(s) preferably comprises from about 0.05 vol. % to about 4.0 vol. % or higher of the coemulsifying agent. The quantity of coemulsifying composition(s) employed may be any suitable amount, depending on the type or characteristics of the reservoir formation. Preferably, the quantity of coemulsifying composition(s) employed is from about I0% by wt. to about 100% by wt. of the emulsifying composition(s), more preferably 20% to 50% by wt. Stated alternatively, the proportion or ratio by wt. of the coemulsifying composition(s) to the emulsifying composition(s) is from 0.10 to 1.0, more preferably from 0.20 to 1.0 to about 0.50 to 1.0. The object is not so much to formulate an oil-in-aqueous phase with the coemulsifying composition(s), but to provide a coemulsifying composition(s) having an appropriate quantity of coemulsifying agent such that when the coemulsifying composition(s) is injected into the hydrocarbon-bearing reservoir ahead of the emulsifying composition(s), it is adsorbed on or to or by the reservoir rock or formation in order to further or ultimately reduce or prevent or further curtail any possibility of adsorption of the subsequent following emulsifying composition(s) onto the reservoir rock or formation. It should be understood that obviously, some oil-in-aqueous phase emulsion will be formulated with the coemulsifying composition(s), but the primary purpose of the coemulsifying composition(s) is to coat and adsorb onto the reservoir rock or formation to cut down or reduce the quantity of emulsifying composition(s) to be employed, thus making the process more economical since the emulsifying composition(s) is typically more expensive than the coemulsifying composition(s). The employment of the coemulsifying composition(s) in combination with the emulsifying composition(s) is not only more economical, but there is also an improvement in the recovery of the hydrocarbon, especially when the emulsifying composition(s) is followed by steam and the well/wellbore is shut-in for a soak period. By way of example only, if a combined 5000 gal. quantity of both coemulsifying composition(s) and emulsifying composition(s) is employed in a ratio of from about 0.1 to 1.0 in the process of this invention for recovering oil from a subterranean hydrocarbon-bearing reservoir, there is a 2 to 40% improved recovery than if 5000 gal. of the emulsifying composition(s) or the coemulsifying composition(s) is employed alone or in a ratio other than 0.1 to 1.0.

The method of this invention employing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), may be practiced in any suitable reservoir and the invention is not to be unduly restricted to a particular type of reservoir or formation. For example, the reservoir may be a sand formation or a rock formation. It may be fractured or unfractured. The hydrocarbon or oil in the reservoir may be any weight or gravity, but as indicated the alkylphenol compounds having general formulas (7) and (8) are particularly suitable for heavy oils or hydrocarbon. The method for this embodiment of the invention has been proven particularly useful in an unconsolidated shallow sand formation and is potentially useful in any subterranean reservoir with little or no natural drive, particularly reservoirs with relatively high permeability and relatively high oil/water ratios in the produced fluids. It is to be appreciated that the success of the method will vary with the specific geology of a particular reservoir; for instance, factors such as reservoir porosity or permeability will influence the extent of penetration of the emulsifying composition(s) into the reservoir and the effectiveness of oil-in-aqueous phase displacement and recovery.

The method of this invention employing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), may be employed in either primary, secondary, or tertiary recovery. Primary recovery is dependent on the driving forces provided by the gases and connate waters existing in contact with the oil in the reservoir. Before the natural driving forces required for primary recovery are depleted, problems are sometimes encountered which prevent the removal of hydrocarbon from the formation itself or from the wells drilled into it. For example, materials such as paraffins, waxes, and asphalts can accumulate in the formation and the wellbore, restricting or blocking the flow of oil. The ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), have been developed and employed in the method of this invention such as to remove the flow-restricting materials. Following a primary recovery, the compounds having general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), may be used in the method of this invention as a secondary energy source required for continued production of oil from hydrocarbon-bearing formations. A conventional secondary recovery method usually entails injecting fluids into Wells to drive oil out of the reservoir, and typical secondary oil recovery methods are waterflooding and immiscible gasflooding. The method of this invention would employ the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), to flood the zones to form oil-in-aqueous phase emulsions with any hydrocarbons remaining after primary recovery. Tertiary oil recovery, also known as enhanced oil recovery (EOR), is recovery of oil which cannot be recovered by either primary or secondary methods. The aim of tertiary oil recovery methods is to reduce oil saturation. One method of achieving this aim is by reducing the viscosity of the oil remaining in the reservoir. Viscosity reduction is achieved through the application of heat or by the injection of fluids such as the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s). Tertiary oil recovery methods employing heat have been performed in single wells and are referred to as thermal "huff and puff" methods. A fireflood "huff and puff" method is a thermal "huff and puff" method. Other thermal "huff and puff" methods have involved the injection of steam into a formation where it is allowed to soak for a time sufficient to lower the viscosity of the oil remaining in the reservoir. The reduction in viscosity permits the oil to be pumped back out of the same well through which steam was injected. One embodiment of the method of this invention as previously explained above is a variation on the steam "huff and puff" enhanced oil recovery method.

In one preferred embodiment of this invention for formulating oil-in-aqueous phase emulsion with the compounds having general formulas (7) and (8), or the same in combination with the initial injection of the coemulsifying composition(s), and with a viscous, heavy crude oil in a petroleum reservoir, at least one well is extended from the earth's surface down into the bottom of a subterranean petroleum reservoir that contains the viscous heavy crude oil. After the well has been extended, the in situ oil-in-aqueous phase emulsion operation is commenced for a predetermined period of time in proximity to the bottom of the subterranean petroleum reservoir by injecting emulsifying composition(s) containing the alkylphenol compounds having the general formulas (7) and (8) into the injection well in order to establish an emulsion forming zone. Alternatively, as has been previously indicated, prior to or before the injection of the emulsifying composition(s), the coemulsifying composition(s) is injected directly through the well/wellbore and into the hydrocarbon-bearing reservoir. After an emulsion forming zone has been established in accordance with the desired pressures and temperatures, the emulsion forming zone is moved and distributed outwardly away from the injection well by the hot water and/or steam. After the emulsion forming zone has been positioned at a desired distal location, the injection of the hot water and/or steam is terminated, and the injection well is shut-in for a predetermined period to permit the hydrocarbon/viscous heavy crude oil in the petroleum reservoir to undergo a soak period in order to formulate the oil-in-aqueous phase emulsion and to decrease the viscosity of viscous heavy crude oil imposed over or underlying the steam treated zone. As the viscosity of the viscous heavy crude oil decreases, it begins to flow downwardly into the emulsion forming zone in order to form additional oil-in-aqueous phase emulsion. The formulated oil-in-aqueous phase emulsion may be produced from one or more production wells that are drilled down into the bottom of the petroleum reservoir where the formulated oil-in-aqueous phase emulsion accumulates and resides. The number of production wells that may be drilled may vary in accordance with any configuration desired, such as an inverted five-spot or nine-spot or a line drive mode of operation. In an inverted five-spot mode of operation, the injector well is the center well of the five-spot, and production wells comprise the other four spots of the configuration which resembles the configuration on dominoes or dice from an overhead view. In other words, the injection well is in the center of a square, from an overhead view, with four production wells lying in the corners of the square. The inverted nine-spot mode of operation is similar to the inverted five-spot, that is, the injection well lies in the center of a square, from an overhead view, with four production wells lying in the corner of the square and four more production wells each lying in a line between two corner wells. In a line-drive mode of operation, a plurality of injection wells are employed to inject steam and/or emulsifying compositions into a formation causing advance of the emulsion forming zone in a more or less straight line parallel to a line intersecting the plurality of injection wells. This mode of operation may be enhanced through the use of horizontal bore holes in the formation for both injection and production.

The length of the soak period for this invention will vary depending on the characteristics of the heavy crude oil within the petroleum reservoir, particularly viscosity of the reservoir oil. We have discovered that the soak period should be from at least about one day to about one year, more preferably one to ten days. During the soak period, the oil-in-aqueous phase emulsion continues to be formulated and the viscosity of the heavy crude oil imposed over or overlying the emulsion forming zone decreases and the oil starts to flow downwardly (i.e., by gravity) in order for the flowing oil to be emulsified. Thermally cracked products resulting from high temperature steam are available to be emulsified into the oil-in-aqueous phase emulsion.

After the soak period has been terminated, after a predetermined amount of time which would be the time necessary to allow the majority of the heavy crude oil to be emulsified into the oil-in-aqueous phase emulsion and to flow downwardly in order to be converted and/or emulsified, the wells are re-opened in order to produce oil-in-aqueous phase emulsion and upgraded crude oil from the bottom of the petroleum reservoir. It should be understood that the oil-in-aqueous phase emulsion and the upgraded crude oil in the bottom of the reservoir may be produced from any production well by any conventional means utilized in that secondary or tertiary recovery means.

It has been discovered that if, prior to forming the oil-in-aqueous phase emulsion, the emulsifying composition(s) is heated to above the P.I.T. (e.g. above 200.degree. F., preferably 200.degree. F. to 600.degree. F., more preferably 250.degree. F. to 400.degree. F. and subsequently followed by cooling to below the P.I.T., the oil-in-aqueous phase emulsion formed after cooling to below the P.I.T. has a greater or enhanced stability compared to an oil-in-aqueous phase emulsion formed where the emulsifying composition(s) was not heated to above the P.I.T. Thus, in another embodiment of the present invention, the emulsifying composition(s) is initially heated to a temperature above the P.I.T. for the oil-in-aqueous phase emulsion to be formed, such as a temperature from about 200.degree. F. to about 600.degree. F.; and subsequently injected through a well/wellbore and into a subterranean hydrocarbon-bearing reservoir or formation having a hydrocarbon. The heating of the emulsifying composition(s) can be accomplished by any suitable means and at any suitable location, such as on the surface of the earth, or while traveling down the well/wellbore and employing the use of any temperature gradient, or while being injected into the reservoir or formation itself. One preferred means for heating the emulsifying composition(s) is to accompany the emulsifying composition(s) with steam, which typically would have a temperature of from about 212.degree. F. to about 600.degree. F., preferably from about 215.degree. F. to about 400.degree. F. As the emulsifying composition(s) travels down the well/wellbore, the steam commingles and mixes intimately with the emulsifying composition(s) causing the temperature of the latter to inherently rise, preferably above the P.I.T. Obviously, the amount or degree of temperature elevation primarily depends on the temperature of the steam. The hotter the steam the higher is the temperature elevation of the emulsifying composition. The steam also provides a transport medium which assists in dispersing and carrying the emulsifying composition(s) into and throughout the reservoir or formation for contacting and mixing with the in situ hydrocarbon. With the temperature of the emulsifying composition(s) being above the P.I.T., no oil-in-aqueous phase emulsion is formulated when the emulsifying composition(s) contact and mix with in situ hydrocarbon. After the desired quantity of above P.I.T. emulsifying composition(s) has been injected into the reservoir or formation, steam or steam and hot water continually follows the emulsifying composition(s)/steam mixture to distribute the above P.I.T. emulsifying composition(s) at desired distances throughout the reservoir or formation for contacting the in situ hydrocarbon. As the dispersed emulsifying composition(s) cools below the P.I.T. while in contact with in situ hydrocarbon, oil-in-aqueous phase emulsion formulates with a greater or enhanced stability than had not the emulsifying composition(s) been heated above the P.I.T. The cooling of the emulsifying composition(s) to below the P.I.T. typically takes place after the well/wellbore has been shut-in and during the soak period. After all of the emulsifying composition(s) has cooled to below the P.I.T. and enhanced stability oil-in-aqueous phase emulsion has formulated, the well/wellbore is reopened to recover the enhanced stability oil-in-aqueous phase emulsion.

Another preferred means for heating the emulsifying composition is to heat the aqueous phase of the emulsifying composition to above the P.I.T. prior to mixing with the emulsifying agent such that the emulsifying composition(s) to be injected into the reservoir has a temperature above the P.I.T. This above P.I.T. emulsifying composition is distributed through the reservoir or formation with steam and/or hot water. When the emulsifying composition(s) cools below the P.I.T. while in contact with hydrocarbons, oil-in-aqueous phase emulsion(s) formulates in situ with greater or enhanced stability.

A further preferred means for heating the emulsifying composition is to accompany the emulsifying composition(s) with hot water (instead of steam) which, as previously indicated, could have a temperature of 150.degree. F. to 250.degree. F. (depending on the pressure) or even higher provided the hot water does not vaporize into steam. Preferably the hot water would be of such temperature as to raise the overall temperature of the emulsifying composition above the P.I.T. The quantity of hot water (or steam) should be targeted such that the eventually formed oil-in-aqueous phase emulsion has a selected aqueous phase and connate water content of from about 10 percent to about 70 percent by weight aqueous phase and connate water and a viscosity sufficiently low such as to be recovered from the reservoir or formation. As the mixture of hot water and emulsifying composition(s) is injected into the reservoir, it contacts the hydrocarbon (and connate water) at a temperature above the P.I.T.; thus, no oil-in-aqueous phase formulates until the emulsifying composition(s) begins to cool during the soak period to a temperature below the P.I.T. As was previously indicated above, the mixture of emulsifying composition(s) and hot water is followed before the soak period by steam and/or hot water to distribute the above P.I.T. emulsifying composition(s) at preferred locations and distances throughout the reservoir for coming in contact with distal hydrocarbons. After shutting in the well/wellbore and soaking for a desired suitable period, such as one to ten days or longer, the well/wellbore is reopened to recover enhanced, stable oil-in-aqueous phase emulsion.

As was-previously indicated, the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8) can be employed for mobility control in steamflood/waterflood operations and to improve sweep efficiencies. The efficiency of a waterflood operation is severely affected by the channeling of the injected water through a high permeability zone or a high water saturation zone (e.g. a bottom water). Furthermore, the economics of many steamflood enhanced oil recovery projects are strongly affected by steam override (gravity segregation) and steam channeling. Cores taken from heavy oil reservoirs at the termination of a steam drive clearly show this upward migration of the steam and consequent segregation of the displacing and displaced fluids. Oil-in-aqueous phase emulsions formulated with the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with initially injecting oil-in-aqueous phase emulsions formulated with the coemulsifying composition(s) in accordance with the previously mentioned procedure above, can be used to increase the efficiency of a waterflood operation by plugging the high water mobility zone and following this plugging procedure with waterflooding. As the oil-in-aqueous phase emulsion is being injected into the reservoir formation, a greater quantity of the emulsion enters the more permeable zones since it will take the path of last resistance. As this occurs, the flow of subsequent following water becomes more restrictive within the reservoir formation and water begins to flow into less permeable zones which contain residual hydrocarbons, resulting in greater sweep efficiency. The oil droplets contained in the oil-in-aqueous phase emulsion can create blockage in high permeability zones by the lodging of the oil droplets within pore throats of the reservoir formation. The oil droplets not only block pores of throats, especially those smaller than the size of the oil droplets, but they are also captured in pore walls and in crevices to create an ensemble of oil droplets crowding together in a single pore throat.

Oil-in-aqueous phase emulsions formulated with the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the same in combination with initially injecting oil-in-aqueous phase emulsions formulated with the coemulsifying composition(s), can increase the economic performance of many steamflood operations by plugging the steam-swept override zones or channeling zones with the emulsions in order to direct subsequent following steam to zones of higher oil saturation and, thus, improve the ratio of oil produced to steam injected. The channeling or steam-swept override zones are zones of high permeability and if not blocked off or plugged will consume a large portion of injected steam to ultimately affect the economic performance of the steamflooding operation. After the oil-in-aqueous phase emulsions have plugged these more permeable zones, the mobility of the steam into high permeability zones is reduced and injected steam flows into the less permeable zones containing residual hydrocarbons, commencing a thermal sweep-out of such residual hydrocarbons.

The formulation of oil-in-aqueous phase emulsions with the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8), or the coemulsifying composition(s) containing the coemulsifying agent(s), may be formulated by any of the procedures indicated herein and at any desired suitable location. By way of example only, the oil-in-aqueous phase emulsion can be formed on the surface of the earth, between the surface of the earth and the bottom of the well, or in proximity to the bottom of the well contiguous to a perforated zone, all for subsequent injection into the reservoir formation. The oil-in-aqueous phase emulsion can be formed spontaneously in situ for subsequent passage or movement into the desired zones by a drawing/mobilizing agent, such as water and/or steam and/or gas. Where and/or how the oil-in-aqueous phase emulsions are formulated is not critical since the emulsifying composition(s) containing the ethoxylated alkylphenol compounds having the general formulas (7) and (8) are compatible with fresh water or brine (i.e., up to 10%, or 100,000 ppm, NaCl and/or CaCl.sub.2), are chemically stable at reservoir conditions, are thermally stable at elevated temperatures, and are essentially immune from extremes in pH, oxygen content, metal content and other impurities present in the reservoir formation and which do not adversely affect the stability of the emulsifying composition(s). It should be understood that after the waterflooding or the steamflooding operations have been terminated, the oil-in-aqueous phase emulsion may be recovered by conventional techniques, such as by natural drives from the low-viscosity emulsion flowing out of the high permeability zones and into well/wellbore.

Any of the emulsifying composition(s) of this invention may be used in downhole emulsification which allows increased production from a heavy crude or bitumen well. Downhole emulsification refers to the formation of a water continuous emulsion in the production tubing of a well producing heavy crude or bitumen. The benefit gained by formation of the emulsion is a great reduction in the viscosity of the crude in the well tubing, allowing a significant increase in the production rate. The factor limiting production in many conventional heavy crude wells is the time required for the sucker rod and pump plunger to fall to their down position after an upstroke. The viscous drag on the rod results in very slow production. The low viscosity of a water continuous emulsion eliminates this constraint. A water continuous emulsion may be formed in the well casing by mixing the crude and brine flowing into the pump with emulsifying composition(s). This operation causes the water to become the continuous phase with the crude being encapsulated as droplets or as larger discrete masses. The free water phase lubricates the contact of the crude with the production tubing and the sucker rod to accomplish the desired reduction in drag. Shear forces are required to form the crude into the separate particles surrounded by water. The flow of the crude, water and surfactant through the passages within the downhole pump provides sufficient shear for this purpose. The relative quantities of crude, water and surfactant flowing into the pump are crucial for proper well operation. If too little water is present at the pump inlet then the resulting viscosity of the water continuous emulsion will not be as low as desired. If the water fraction is too high, then a very low viscosity emulsion will be formed which does not have the capacity to carry formation sand (which is often associated with heavy crude production operations) out of the well. During periods when the well may not be operating, the accumulated sand may settle in the tubing and result in failure to restart the well. The best operation of a downhole emulsification system is obtained with water concentrations in the 15% to 50% range.

The quantity of emulsifying agent employed in the emulsifying composition(s) injected can affect the properties of the produced water continuous emulsion. If too little emulsifying agent is used, an emulsion will not be formed. If excessive emulsifying agent is injected, very small and .stable oil droplets may be formed which are difficult to separate from the emulsion. The desired concentration of emulsifying agent in the total produced fluids is 200 to 1000 parts emulsifying agent per million parts of crude with a preferred concentration of 300 to 500 ppm. Optimal operation of the system is achieved by adjusting the emulsifying agent level so that the low viscosity of water continuous emulsion is achieved without the formation of small oil droplets.

The emulsifying composition(s) added to form oil-in-aqueous phase emulsion may be injected into the system by any suitable means. In the preferred injection system for the embodiment of the invention in FIGS. 16 and 17, a downhole pump and sucker rod (not shown in the drawings) is replaced with a special diluent injection pump, generally illustrated as 400, and a hollow sucker rod assembly 402. The injection pump 400 is secured to the end of the hollow sucker rod assembly 402 as best illustrated in FIG. 17, and both are removably disposed through a tubing 404 which is generally concentrically situated in a casing 406 perforated at 408 for the passage of formation fluids. The injection pump 400 comprises a hollow upper plunger 410 secured to a lower end of the hollow rod 402, and a hollow cross over fitting means 412. A hollow lower plunger 414 having a traveling valve 416 integrally connects to the hollow cross over fitting means 412. The tubing 404 has a by-pass conduit 418 connecting from a lower part of the tubing 404 (as best illustrated in FIG. 17) down between the lower portion of the tubing 404 and the casing 406, terminating below or in close proximity to a standing valve 420. On the surface of the earth (see FIG. 16), a hollow flexible hose 422 connects to the hollow rod 402. Water from water tank 424 is pumped via pump 426 through hose 422. Emulsifying agent(s) is introduced into the hose 422 to form emulsifying composition(s) which is pumped down the hollow sucker rod assembly 402, through passageways indicated by arrows A in FIG. 17 and into the by-pass conduit 418. As the emulsifying composition(s) leaves conduit 418, it mixes with crude passing through perforations 408 from the reservoir formation to form oil-in-aqueous phase emulsion which is subsequently pumped (or sucked) through standing valve 420 and through valve 416 into the lower plunger 414 via arrows B and through valve 416 via arrow C, into the hollow cross-over 412 via arrow D, into the hollow upper plunger 410 via arrow E and passageways indicated as dotted lines P in FIG. 17, and out of the hollow upper plunger 410 via arrow F into the annulus between the tubing 404 and the hollow sucker rod 402. On the surface of the earth, the oil-in-aqueous phase emulsion leaves the annulus between the tubing 404 and the hollow sucker rod 402 through conduit 430 to be discharged into a heated production tank 432 where most of the water/brine is separated from the emulsion. This water/brine is passed through conduit 434 into the water tank 424 for recycling into the injection system as it contains a significant portion of the emulsifying agent(s) and reduces the quantity of make-up emulsifying agent(s) required.

In the preferred injection system for the embodiment of the invention in FIG. 18, a concentrated emulsifying composition(s) 431 is metered continuously directly into the annulus between the well casing 406 and the tubing 404. In contrast to the embodiment in FIGS. 16 and 17, no changes were made to a conventional downhole pump, illustrated generally as 450 in FIG. 18, a solid conventional sucker rod 452, or any of the other conventional components. The emulsifying composition(s) 431 drips or flows intermittently or otherwise into the annulus between the casing 406 and the tubing 404, mixes with the formation fluids at the bottom of the hole in the casing annulus, and eventually reaches an inlet of the downhole pump 450 where a water continuous emulsion is formed to be pumped up the hollow tubing 404 for discharge through conduit 430. In the injection system for the embodiment of the invention in FIG. 19, which is a variation of the method described for FIG. 18, the addition of emulsifying composition(s) 431 into the casing annulus is on a batch basis rather than continuously. A head H of emulsifying composition(s) is created. The emulsifying composition(s) 431.sup.R is blended with formation fluids in the annulus and is gradually mixed with the crude coming into the well to form a water continuous emulsion. The concentration of the emulsifying composition(s) gradually decreases to a point at which it becomes ineffective. The quantity and frequency of batch emulsifying composition(s) injections is adjusted to maintain a minimum acceptable level of emulsifying composition(s) at the downhole pump inlet. This method may also include the addition of water or brine with the emulsifying composition(s) to increase the water concentration of the production fluid to a minimal level of approximately 20% which is required for formation of the desired low viscosity emulsion. The addition of a large batch of water and emulsifying composition(s) into the well casing has a further benefit in comparison to the injection embodiments in FIGS. 16 and 17 and 18. The benefit is the result of raising the fluid level in the well casing, a point of which causes the fluid in the casing annulus to flow through perforations 408 and into the reservoir adjacent to the well. This fluid, containing emulsifying composition(s) solution, cleans the reservoir in this area and improves inflow into the well. As a result, the pressure drop related to crude and water flow into the well is reduced and a higher fluid level is sustained in the casing. Another preferred injection system is the embodiment depicted in FIG. 20 and is similar to FIG. 18, but employs the use of a separate tube 460 parallel to production tubing 404. Emulsifying composition(s) is conducted or pumped through flexible hose 422 (or solid conduit), and into and through the tube 460 which terminates in close proximity to perforations 408. The emulsifying composition(s) commingles with oil leaving the reservoir formation through perforations 408 to form an emulsion that is pumped to the surface of the earth through production tubing 404 via pump 450.

As has been previously stated, the emulsifying agent(s) of this invention has to be mixed with a water or the pipeline-transportable oil-in-water emulsion(s) of this invention cannot be formulated. The emulsifying agent(s) should not contact the produced hydrocarbon crude directly before being admixed with water. Stated alternatively, the emulsifying composition(s) of this invention which is to be admixed or combined with the produced hydrocarbon crude have to contain water, or the oil-in-water emulsion(s) of this invention will not be produced to be pipeline-transportable.

As has also been previously stated, the freezing point of the emulsifying composition(s) and/or the oil-in-water emulsions may be lowered by the addition of a compound which lowers the freezing point of water, which for the purpose of this invention is preferably ethylene glycol. The oil-in-water emulsion(s) of this invention are water continuous and through the addition of ethylene glycol into the emulsifying composition(s), the freezing point of the continuous phase (i.e. water) of the oil-in-water emulsion(s) is lowered. Preferably, ethylene glycol is added to the emulsifying composition(s) such that the emulsifying composition(s) and/or the water continuous phase of the oil-in-water emulsion(s) comprise from about 0.5% by wt. to about 80% by wt. ethylene glycol, more preferably from about 0.5% by wt. to about 30% by wt.

In order to form a more stable oil-in-water emulsion (or water continuous emulsion) when the produced hydrocarbon crude is Athabasca bitumen, the water or aqueous phase preferably has a pH of above 4.0, preferably from about 6.0 to about 13.0, such as 7 to 9 and 6 to 8. This is especially true when brine is employed as the aqueous phase. If brine is being utilized, salinity becomes another factor. It has been found that with brine as the aqueous additive for the produced hydrocarbon crude, the salinity of the brine should be at least about 1.5% by wt. salt (i.e. NaCl). It should be pointed out that no upper limit on salt concentration has been determined and may be that quantity of salt which supersaturates the brine, or that upper amount of salt which goes into solution.

More stable oil-in-water emulsion(s) are formed, especially when the produced hydrocarbon crude is Athabasca bitumen, with the use of the biopolymer xanthan which is an additional stability enhancer. Biopolymer xanthan is added to the emulsifying composition(s) such that the emulsifying composition(s) and/or the water continuous phase of the oil-in-water emulsion(s) such that the oil-in-water emulsion(s) comprises biopolymer xanthan in a ratio of from about 25 ppm to about 5,000 ppm by weight of the produced hydrocarbon crude. Stated alternatively, biopolymer xanthan is provided in a concentration of from about 25 to about 5,000 ppm by weight of the produced hydrocarbon crude.

Xanthan has outstanding resistance to shear degradation, and is insensitive to waters with high salt content. Xanthan contains D-glucose, D-mannose, and D-glucuronic acid. It is believed to have a cellulose-like backbone composed of repeating .beta.-D-(1-4) glucose units with mannose and glucuronic acid present in side chains, and mannose partially modified with acetyl and pyruvate ketol groups.

Xanthan molecular weight is reported to be greater than one million. The biopolymer exists in solution as a helix in native form. The present accepted structure for xanthan is as follows: ##STR19##

Biopolymer xanthan may be purchased commercially as FLOCON.sub.R Biopolymer 4800 from Pfizer Inc.

In another embodiment of the present invention, the viscosity of the effluent oil-in-water emulsion(s) through and/or from conduit 110, or in the emulsion tank 122, may be controlled and/or reduced to facilitate the transportation of the oil-in-water emulsion(s) of this invention. This result is achieved by tailoring the droplet size distribution in the produced oil-in-water emulsion. Lower viscosity for the oil-in-water emulsion(s) reduces the power required for pipeline pumping operations, and also decreases the stress placed on the oil-in-water emulsion(s) which could cause oil droplets in the oil-in-water emulsion(s) to coalesce and increase in size. Formation of water continuous emulsions with a tailored oil droplet size, results in a lower emulsion viscosity for the effluent oil-in-water emulsion(s).

The viscosity of a suspension of oil particles or oil droplets is a function of the viscosity of the water continuous phase, the concentration of the oil particles, and the distribution of oil particle size. An approximation of the viscosity of an oil-in-water emulsion is given by the following equation: ##EQU4## where .mu.=oil-in-water emulsion viscosity (cs)

.mu..sub.o =viscosity of the water continuous phase (cs)

.phi.=volume fraction of the dispersed oil phase

.phi..sub.p =maximum packing fraction for the emulsion oil droplet size distribution

The equation illustrates that the viscosity of an oil-in-water emulsion may be reduced if the oil droplet size distribution results in a larger maximum packing fraction. This reduction may be accomplished by forming the oil-in-water emulsion such that a wide range of oil droplet sizes results, or by the formation of a bimodal oil droplet size distribution. By way of example only, in comparison to a monodisperse oil-in-water emulsion with o=0.5, a bimodal oil-in-water emulsion with an oil droplet size ratio of 5 to 1 theoretically has a viscosity reduced by a factor of about 10, assuming spherical and non-interacting oil particles.

The viscosity of the effluent oil-in-water emulsion(s) of the present invention may be controlled and/or reduced by varying the flow rate (and the shear rate) of the mixture of emulsifying composition(s) and the produced hydrocarbon crude through the static shearing and mixing device 108; or alternatively, by splitting (as illustrated FIG. 2) the flow of the mixture of emulsifying composition(s) and produced hydrocarbon crude in conduit 50 into conduit 130 and conduit 132, and flowing the respective split mixture through the conduit 130 and conduit 132 at distinguishable or different shear rates [shear rate =(8.times.velocity in inches/sec.) divided by static mixer diameter in inches]. In order to control these two flow rates and to ensure that the respective shear rates are distinguishable or different, flow rat control valve 134 and flow rate control valve 136 are provided within conduit 130 and 132, respectively. Valves 134 and 136 may be set and controlled such that the shear rates of the respective mixtures of the emulsifying composition(s) and produced hydrocarbon crude through static shearing and mixing means 108A and 108B are indeed different. The shearing and mixing means 108A and 108B may have the same or different diameter. The respective effluent oil-in-water emulsion(s) from static shearing and mixing means 108A and 108B are conducted or transported through conduits 138 and 140, respectively, and into the conduit 110 of FIG. 1 wherethrough the two admixed or combined mixtures are sent to the emulsion tank 122 (see FIG. 1). As illustrated in FIG. 1, before settling into the emulsion tank 122, the temperature of the two admixed emulsion mixtures should be reduced below about 120.degree. F. with heat exchanger 120 in order to increase the stability of the formulated bimodal or multimodal oil-in-water emulsion(s) that has a lower viscosity than either the viscosity of the effluent oil-in-water emulsion(s) in conduit 138 or the viscosity of the effluent oil-in-water emulsion(s) conduit 140. The viscosity of the formulated bimodal oil-in-water emulsion(s) comprising the two effluent oil-in-water emulsion(s) from conduits 138 and 140 is not the average or mean of the viscosity of the two effluent oil-in-water emulsion(s) in conduits 138 and 140, but is lower than either. It is to be understood that while only a pair of parallel static shearing and mixing devices 108A and 108B have been illustrated and represented, three (3) or more parallel devices may be employed within the spirit and scope of this invention.

A bimodal or multimodal oil-in-water emulsion(s) may also be formed in the emulsion tank 122 by varying the flow rate (and the shear rate) of the mixture of emulsifying composition(s) and produced hydrocarbon crude through the static shearing and mixing device 108, and collecting the effluent oil-in-water emulsion(s) produced from the static shearing and mixing device 108 at various flow (and shear) rates in the emulsion tank 122. The collected effluent oil-in-water emulsion(s) produced from various flow rates through device 108 mix and combine in the emulsion tank 122 to form bimodal or multimodal oil-in-water emulsion(s) having a lower viscosity than the viscosity of oil-in-water emulsion(s) produced from the static shearing and mixing device 108 with one flow (and shear) rate. Thus, by way of example only, the viscosity of a bimodal oil-in-water emulsion(s) produced by flowing a mixture of emulsifying composition(s) and produced hydrocarbon crude through device 108 at 50 in./sec. for 10 minutes, and combining the resulting oil-in-water emulsion(s) with the oil-in-water emulsion(s) formulated from subsequently flowing the same mixture through the device 108 at 30 in./sec. for 10 minutes, would be lower than the respective viscosities of the oil-in-water emulsion(s) produced at 50 in./sec. or 30 in./sec.

The size of the oil droplets in the oil-in-water emulsion(s), or in the bimodal oil-in-water emulsion(s), of the present invention tend to increase in size during flow through a pipe, such as pipeline 123. This effect could change the benefits of this invention by changing the oil droplet size distribution through augmentation of the size of oil droplets. To maintain within the pipeline 123, or the like, a bimodal or multimodal nature of the oil-n-water emulsion(s), or to even initially unimodal produce a bimodal or multimodal oil-in-water emulsion(s) from a oil-in-water emulsion, a stream of the multimodal oil-in-water emulsion(s) or the unimodal oil-in-water emulsion(s) may be withdrawn periodically from the pipeline 123, such as through a conduit 142 as illustrated in FIG. 3, and subjected to static shearing and mixing through the use of a flow rate control valve 144 and the static shearing and mixing device 108. As depicted in FIG. 3, flow rate control valve 144 would control the flow rate of any multimodal or unimodal emulsion(s) through the device 108 to reduce the size of the oil droplet within the particular type of emulsion(s) such that when tho effluent oil-in-water emulsion(s) exiting the device 108 through a conduit 146 that is in communication with the pipeline 123 is recombined with the stream of flowing oil-in-water emulsion(s) that has by-passed conduit 142, the bimodal or multimodal nature of the oil-in-water emulsion(s) is re-established. Valve 148 is a variable flow rate valve that restricts the flow of oil-in-water emulsion(s) therethrough such that some of the oil-in-water emulsion(s) flowing through pipeline 123 is forced to flow through conduit 142. valve 150 would control the flow of oil-in-water emulsion(s) and effluent oil-in-water emulsion(s) (from device 108) through the conduit 146. This withdrawal process may be conducted as many times as necessary along the pipeline 123 to maintain water continuous emulsion(s) which have a lower viscosity than if the withdrawal process was not employed. Instead of using static shearing and mixing device 108 in the withdrawal process in order to maintain lower viscosity in the flowing oil-in-water emulsion(s), a centrifugal pump (of the type used in commercial pipelines) may be utilized to reshear the flowing oil-in-water emulsion(s). Any of the mixing and/or reshearing step(s) may be accompanied by the addition of more emulsifying composition(s) if needed.

In another embodiment of the present invention, a bimodal or multimodal oil-in-aqueous phase emulsion(s) may be formed with any of the emulsifying agent(s) of the present invention by varying the residence times and/or the shear rate of the mixture of emulsifying composition(s) and produced hydrocarbon crude in any suitable dynamic shearer and mixer (e.g. a rotor stator mixer, etc.), and collecting the effluent oil-in-aqueous phase emulsion(s) emanating from the dynamic shearer and mixer at various residence times and/or shear rates in any suitable tank or container, such as emulsion tank 122. The collected effluent oil-in-aqueous phase emulsion(s) produced from various residence times and/or shear rates in any suitable dynamic shearer and mixer combine in the emulsion tank 122 to form bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity of oil-in-aqueous phase emulsion(s) produced from one dynamic shearer and mixer having a fixed shear rate and/or residence time of the emulsifying composition(s) and the produced hydrocarbon crude in the dynamic shearer and mixer; or from the static shearing and mixing device 108 with one flow (and shear) rate. Thus, by way of example only, the viscosity of a bimodal oil-in-aqueous phase emulsion(s) produced by positioning for 4 secs. a mixture of emulsifying composition(s) and produced hydrocarbon crude in a dynamic shearer and mixer having a shear field intensity of 500 sec..sup.-1, and combining the resulting oil-in-aqueous phase emulsion(s) with the oil-in-aqueous phase emulsion(s) formulated from subsequently positioning for 4 secs. the same mixture in the same dynamic shearer and mixer having a shear field intensity of 6,000 sec..sup.-1, would be lower than the respective viscosities of the oil-in-aqueous phase emulsion(s) produced with an intensity of 500 sec..sup.-1 or 6,000 sec..sup.-1. Similar results can be obtained by varying the residence time while holding the shear field intensity generally constant or fixed. In this embodiment of the present invention, a bimodal or multimodal oil-in-aqueous phase emulsion(s) may be formed with two or more dynamic shearers and mixers in parallel, or with one (or more) dynamic shearers and mixers in parallel with one (or more) static shearing and mixing device, such as device 108. The collected effluent oil-in-aqueous phase emulsions produced from the two (or more) dynamic shearers and mixers having different shear rates (or shear field intensities) and/or with different residence times for the mixture of emulsifying composition(s) and hydrocarbon crude in the respective dynamic shearers and mixers combine to form bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity than the viscosity of oil-in-aqueous phase emulsion(s) produced from any one of the two (or more) dynamic shearers and mixers. Similarly, the collected effluent oil-in-aqueous phase emulsions produced from one (or more) dynamic shearers and mixers in parallel with one (or more) static shearing and mixing devices combine to form bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity than the viscosity of oil-in-aqueous phase emulsion(s) produced from any single one dynamic shearer and mixer or from any single one static shearing and mixing device. Typically, each dynamic shearer and mixer has a different shear rate (or shear field intensity) and/or the residence times of the emulsifying composition-crude mixture in each dynamic shearer and mixer are distinct from each other. Typically further, each static shearing and mixing device has or produces a different shear rate from the other static shearing and mixing devices. Thus, by way of example only, a bimodal or multimodal oil-in-aqueous phase emulsion may be produced by positioning for a generally known period (e.g. 0.10 sec to 5 mins. or higher) a portion of an emulsifying composition-hydrocarbon crude mixture in a first dynamic shearer and mixer having a predetermined or known shear rate (e.g. a shear field intensity from 50 sec..sup.-1 to about 10,000 sec..sup.-1 or higher) to produce a first oil-in-aqueous phase emulsion having a first viscosity, leaving a remaining portion of the emulsifying composition-hydrocarbon crude mixture that has not been positioned in the first dynamic shearer and mixer. The remaining emulsifying composition-hydrocarbon crude mixture is positioned for a generally known period of time in a second dynamic shearer and mixer (or passed through a static shearing and static mixing device at a predetermined velocity for a predetermined period of time). The second dynamic shearer and mixer has a shear rate that is different from the shear rate of the first dynamic shearer and mixer, and produces a second oil-in-aqueous phase emulsion having a second viscosity. When the first oil-in-aqueous phase emulsion is mixed or commingled with the second oil-in-aqueous phase emulsion, an oil-in-aqueous phase emulsion is produced having a viscosity lower than the first viscosity of the first oil-in-aqueous phase emulsion and lower than the second viscosity of the second oil-in-aqueous phase emulsion. The one or more dynamic shearers and mixers and/or one or more static shearing and mixing devices may be in any relationship to each other, such as in parallel or in series.

The static shearing and mixing device 108 (and 108A and 108B) of this invention may be any static, in-line mixer that is capable of producing the oil-in-water emulsion(s) of the invention. Not any static, in-line mixer may be capable of this production. We have discovered that suitable static shearing and mixing devices 108, 108A, and 108B for this invention are those that employ a stationary baffle means installed within a pipe, conduit, or the like, such that the energy of the flowing mixture of emulsifying composition(s and produced hydrocarbon crude produces the required shearing and mixing to produce the oil-in-water emulsion(s). The stationary baffle means may not be just any baffle means which may give unpredictable mixing efficiency as equipment size and flow conditions change. Also, just any baffle means may provide appreciable shearing the mixing only under turbulent flow conditions, whereas the oil-in-water emulsion(s) of this invention are to be produced under both laminar and turbulent flow conditions.

The static shearing and mixing devices 108, 108A and 108B of this invention are to employ a baffle means that provides precise geometric paths for fluid flow in order to obtain consistent, predictable mixing performance, regardless of the flow rate of the mixture of emulsifying composition(s) and produced hydrocarbon crude, or equipment dimensions. Preferred static shearing and mixing devices 108, 108A and 108B have been determined to be certain of the motionless mixers manufactured by Komax Systems Inc., Long Beach, Calif. and Koch Engineering Company, Inc., Wichita, Kans. The motionless mixers produced by these two companies and suitable in the process of the present invention to produce the oil-in-water emulsion(s) employ a baffle means in a conduit that shears and mixes simultaneously. Similar designs by other manufacturers may work equally well.

A preferred static shearing and mixing device 108 (or 108A or 108B) manufactured by Komax Systems, Inc. is illustrated in FIGS. 4, 5, 6, and 7, and is more particularly described and illustrated in U.S. Pat. No. 3,923,288 which is incorporated herein by reference. Referring in detail now to FIGS. 4-6, there is seen one embodiment for the static shearing and mixing device 108 (or 108A or 108B) of this invention which comprises a conduit 152 having an internal chamber 154 in which a plurality of baffle elements, generally illustrated as 156 and 158, are sized and fitted. Internal chamber 154 is open at the two ends of the conduit 152 such that the mixture of emulsifying composition(s) and produced hydrocarbon crude may pass over and through the plurality of baffle elements 156 and 158 to effect the required shearing and mixing to produce the oil-in-water emulsion(s). A longitudinal axis passes through the length of the chamber 154 which has a generally cylindrical configuration as is illustrated in FIG. 4. Baffle element 156 is shown in greater detail in FIGS. 5 and 7 and is the mirror image of baffle element 158 which is shown in greater detail in FIGS. 6 and 7.

Baffle element 156 comprises a flat generally rectangular central portion 160, the plane of which is to be generally aligned with the longitudinal axis of the chamber 154. A first set of ears 162 and 164 are integrally bound to one side of the central portion 160, and are arcuate and configured at their outer peripheries for a general fit against the internal wall of the chamber 154. The first set of ears 162 and 164 are bent respectively in an upward and downward direction relative to the plane of the central portion 160. A second set of ears 166 and 168 are integrally bound to the opposite side of the central portion 160, and like the first set of ears 162 and 164, are bent upward and downward relative to the plane of the central portion 160. Ears 162 and 168 are located diagonally opposite one another across the central portion 160 and are bent in the same direction relative to the plane of the central portion 160. Likewise, ears 164 and 166 are also located diagonally opposite one another across the central portion 160 and are also bent in the same direction relative to the plane of the central position 160. The outside peripheral edges of the ears 166 and 168 are also arcuate and configured for a general fit to the wall of the chamber 154.

Baffle element 158, as was previously indicated, is a mirror image of the baffle element 156, and in a similar manner comprises a central portion 170, a first set of ears 172 and 174, and a second set of ears 176 and 178. Ears 172 and 178, as well as ears 174 and 176, are diagonally positioned across the central portion 170 with respect to one another and are bent in the same direction relative to the plane of the central portion 170.

The angle between ears 162-164, 166-168, 172-174, and 176-178 may be any suitable angle that can provide the shearing and mixing of the mixture of emulsifying composition(s) and produced hydrocarbon crude to produce the oil-in-water emulsion(s) of this invention. Preferably, the angle between the respective set of ears is from about 30.degree. to about 120.degree..

In a preferred embodiment for the mixing device 108 n FIGS. 4-7, a plurality of baffle elements 156 and 158 are employed in the conduit 152 in an alternating fashion, as illustrated in FIG. 4. The baffle elements 156 and 158 may be spacedly positioned with respect to each other, or preferably, as illustrated in FIG. 4, in an abutting relationship with respect to each other.

When the baffle elements 156 and 158 are in an abutting relationship, ears 172 and 174 of baffle element 158 inter-mesh and/or overlap with ears 166 and 168 of baffle element 156. Similarly, ears 162 and 164 of element 156 inter-mesh and/or overlap with ears 176 and 178 of element 158; all as illustrated in FIG. 7. The total number of baffle elements 156 and 158 used depends on the viscosity of the produced hydrocarbon crude and the degree of mixing desired for the emulsifying composition(s) and the produced hydrocarbon crude. Typically, 6 to 8 baffle elements would be employed in the conduit 152.

When at least one each of the baffle elements 156 and 158 are installed in conduit 152 in an abutting relationship, there is a shearing and a mixing action taking place on the mixture of emulsifying composition(s) and produced hydrocarbon crude that is being passed in direction of the arrow in FIG. 1 through the conduit 152. A counter-clockwise velocity vector or rotational vector is imposed by ears 166 and 168 of element 156 to back-mix the emulsifying composition(s) and the produced hydrocarbon crude and eliminate the streaming or tunneling effects that can occur with conventional static mixers. The central flat portion 160 transforms the counter-clockwise or rotational vector to a lateral or radial vector. After the mixture of emulsifying composition(s) and the produced hydrocarbon crude passes the central flat portion 160, ears 162 and 164 impose an additional counter-clockwise or rotational velocity to the mixture which adds somewhat to the lateral or radial vector that is being produced by the central flat portion 160. Ears 162 and 164 impose a substantially outward directed radial velocity vector, whereas ears 166 and 168 impose a substantially inward directed radial velocity vector, on the mixture of emulsifying composition(s) and produced hydrocarbon crude that is moving longitudinally through the conduit 152. When the mixture leaves baffle element 156 and is passed over baffle element 158, the ears 176 and 178 and 172 and 174 impose both a clockwise rotating velocity vector, as well as a generally inward and outward radial vector, respectively.

FIGS. 8-12 shows another embodiment for the baffle means which is to be fitted into the conduit 152 having the chamber 154 to define the static shearing and mixing device 108. The baffle means of FIGS. 8-12 comprises a plurality of generally identical baffle elements, each generally illustrated as 180, that are interbound with one another.

Each baffle element 180 comprises a central part 182 which is flat and generally rectangular with a plane that is to be generally aligned with the longitudinal axis of the chamber 154. Each baffle element 180 also comprises a flat generally rectangular first part 184 and a flat generally rectangular second part 186. The respective planes of the first part 184 and the second part 186 are generally normal with the longitudinal axis of the chamber 154 and the plane of the central part 182. When the baffle elements 180 connect with one another, the first part 184 of one baffle element 180 attaches integrally to the second part 186 of another baffle element 180, as illustrated in FIG. 9.

Each baffle element 180 also comprises a first pair of arms 188 and 190 forming a generally V-shape and extending from one half (i.e. the upper half relative to when the central part 182 is situated as in FIG. 8) of the central part 182 to the first part 184 where it binds therewith. A channeling member, generally illustrated as 192, extends from the first part 184 to another half (i.e. the lower half relative to when the central part 182 is situated as in FIG. 8) of the central part 182. The channeling member 192 includes a base 194 and a channeling partition 196 that secures to and is generally normal to the base 194, and attaches to the other half of the central part 182. As illustrated in the drawings, there is one opening above the partition 196 and underneath arm 188, and another opening between the base 194 and underneath the arm 190.

Between the second part 186 and the central part 182 on the other side of the central part 182 is an inverted mirror image of the pair of arms 188-190 and the channeling member 192 including the base 194 and the partition 196. More specifically, on the other side of the central part 182 there is seen a second pair of arms 198 and 200 forming a generally V-shape and extending from one-half (i.e. the lower half relative to when the central part 182 is situated as in FIG. 8) of the central part 182 to the second part 186 where they bind thereto. A channeling member, generally illustrated as 202, extends from the second part 186 to another half (i.e. the upper half relative to when the central part 182 is situated as in FIG. 8) of the central part 182. Similar to channeling member 192, channeling member 202 comprises a base 204 and a channeling partition 206 that is bound to the base 204 in a normal relationship, and attaches to the other half of the central part 182. There is one opening below the partition 206 and above the arm 200, and another opening between the base 204 and above the arm 198.

FIG. 13 represents another embodiment of an end for each of the baffle elements 180. In this embodiment, the channeling member 192 is positioned on the opposite side of the central part 182. The first pair of arms 188 and 190 form a generally V-shape and extend to the upper half of the central part 182 and binds therewith. The channeling member 192 extends from the first part 184 down to the lower half of the central part 182 and comprises the base 194 and the channeling partition 196 that attaches normally to the base 194. Partition 196 also attaches to central part 182 and tapers towards and attaches to the first part 184 as well as the arm 188. There is an opening above the partition 196 and below the arm 188, and another opening between the base 194 and below the arm 190.

By employing the baffle element 180 within the conduit 152, it is believed that a number of mixing actions are provided for the mixture of emulsifying composition(s) and produced hydrocarbon crude. A dividing action for the mixture is provided between the opening above the partition 196 and underneath arm 188 and the opening between the base 194 and underneath the arm 190 (see FIG. 11). A cross-current mixing is also provided by the same two openings as illustrated in FIG. 12. Another mixing action is illustrated in FIG. 10 and is back-mixing and counter-rotating vortices. Eliptical vortices rotating in opposite directions are produced on both sides of the central part 182 and eliminates the streaming or tunneling effects associated with other static mixing devices. In back-mixing, the mixture of emulsifying composition(s) and produced hydrocarbon crude is orbited in the vortex from the front to the back of an element before continuing downstream.

Another embodiment of the static mixing device 108 which can be employed in the process of this invention is manufactured by Koch Engineering Company, Inc., Wichita, Kans. and is illustrated in FIGS. 14 and 15. This embodiment of the static mixing device 108 is more particularly described in U.S. Pat. No. 3,785620 which is incorporated herein by reference thereto. The static mixing device 108 for this embodiment of the invention comprises a plurality of baffle elements 208A and 208B which are substantially identical to each other. Baffle elements 208A and 208B are aligned within the conduit 152 in a contiguous generally abutting relationship with each baffle element 208B offset at approximately 90.degree. relative to each baffle element 208A (see in FIG. 14 where the baffle elements 208A and 208B are spacedly positioned for clarity).

Referring to FIG. 15, each baffle element 208A and 208B has corrugated lamellas 210 which are welded to one another to form the particular baffle element, either 208A and 208B. As shown, different sizes or lengths of individual lamellas 210 are used which increase from the two outsides toward the middle so that a generally cylindrical shape results. The lamellas 210 are in a parallel relationship to the longitudinal axis of the conduit 152 and are preferably made of a sheet metal which does not corrode when contacted with the produced hydrocarbon crude and emulsifying composition(s). The corrugations of each lamella 210 are of substantially equal slope, with about 45.degree. being the preferred slope of each corrugation such that when the corrugated lamellas 210 are adjoined to one another (such as by welding), a plurality of open, intersecting channels at 45.degree. to the longitudinal axis of the conduit 152 is formed.

The mixture of produced hydrocarbon crude and emulsifying composition(s) enter the conduit 152 and are split into individual streams in the series of open, intersecting channels for fluid flow. These channels provide strong transversal flow and fluid exchange at the wall of the conduit 152. At each channel intersection, a part of the mixture of produced hydrocarbon crude and emulsifying composition(s) shears off into the crossing channel.

As was previously indicated, baffle elements 208A and 208B are positioned 90.degree. relative to each other, so two-dimensional mixing takes place over the first baffle element (i.e. either 208A or 208B) and three-dimensional mixing over all successive baffle elements. Three-dimensional mixing ensures uniformity in the produced oil-in-water emulsion(s) leaving the conduit 152. Thus, the baffle elements 208A and 208B suitably mix the mixture of produced hydrocarbon crude and emulsifying composition(s) in longitudinal and transverse directions by directing the part-flows of the mixture in a plurality of criss-crossing zig-zag paths through the length of the baffle elements 208A and 208B. The various mixing actions obtained are such that oil-in-water emulsion(s) is easily and rapidly obtained over a relative short length for conduit 152.

Through the use of the emulsifying agent(s) in combination with other features of the invention, oil-in-water emulsion(s) are formulated which contain a strong shear stability, enabling them to be suitable candidates for the pipeline transport of produced hydrocarbon crude, especially for Athabasca bitumen. One physical disadvantage inherent in Athabasca bitumen is its very high viscosity (e.g. about 20,000 cp at 100.degree. F.; 300 cp at 200.degree. F.). This physical fact imposes that the transport of this raw material by conventional pipeline at ambient temperatures is impossible. The alternative use of a diluent naphtha, or the like, is unsuitable due to the cost and long-term availability. The ability to transport Athabasca bitumen over long distances by conventional pipeline technology to existing facilities would reduce the production costs required for on-site upgrading of this petroleum source. The oil-in-Water emulsion(s) formed in accordance with the invention are thermally stable and exhibit a strong shear stability.

The static shearing and mixing device 108 may be used to control the oil droplet size in the oil-in-water emulsion(s) of this invention. Generally, the further an oil-in-water emulsion(s) has to be transported through a pipeline, the smaller the oil droplet size in the oil-in-water emulsion(s) should be since the oil droplets in the oil-in-water emulsions tend to coalesce and augment as the emulsion(s) travel through a pipeline.

The intensity of the shear field on the mixture of emulsifying composition(s) and produced hydrocarbon crude within the static shearing and mixing device 108 is proportional to the rate of flow of the mixture through the device 108. As the shear rate (and the rate of flow) is increased through the operating range, the size of oil droplets from the produced hydrocarbon crude become progressively smaller. The shear rate or the rate of flow of the mixture of emulsifying composition(s) and produced hydrocarbon crude through the mixer should be large enough to impart sufficient shear on the mixture to produce an oil-in-water emulsion(s), but not too large as chaotic mixing can cause the oil droplets to recoalesce before being stabilized in the water continuous phase of the oil-in-water emulsion. In a preferred embodiment of the invention, the flow rate of the mixture of the emulsifying composition(s) and the produced hydrocarbon crude through the device 108 is from about 20 in./sec. to about 140 in./sec.

The oil droplet size within an oil-in-water emulsion(s) may be predicted by the following equation:

where d is the volumetric mean oil droplet size in microns; C is a constant ranging from about 750 to about 1,500, and represents a multiplier contributing to the absolute disposition in volumetric mean droplet size of the oil; D is the internal diameter in inches for the device 108; N.sub.we is the dimensionless Weber Number for the fluid flowing through the device 108 and ranges from about 50 to about 30(10.sup.6); a is an exponent which is from about 0.3 to about 1.2, preferably about 0.6; and b is also an exponent ranging in value from about 0.2 to about 0.8, preferably about 0.4. The exponents a and b are constants, which account for the relative variation in the volumetric means droplet size of the oil.

N.sub.we is the Weber Number, a commonly used dimensionless number relating shear forces imparted on the oil droplet to the cohesive forces holding the oil drop together, defined as ##EQU5## where D is the internal diameter in inches of device 108; v is the velocity in inches per second of the fluid flowing through the device 108; p is the oil-in-water emulsion density in lbs. per cubic foot; and .delta. is the interfacial tension for the oil-in-water emulsion in dynes per cubic centimeter. The oil-in-water emulsion density p ranges from about 40 lbs./ft.sup.3 to about 70 lbs./ft.sup.3. The interfacial tension for the oil-in-water emulsion ranges from about 0.25 dynes/cm..sup.3 to about 25 dynes/cm.sup.3. For a further and more comprehensive discussion of the formula to predict oil droplet size and the defined Weber Number see Industrial Engineering Chemistry Process Design & Development, Vol. 13, No. 1, 1974 by Stanley Middleman, which is entirely incorporated herein by reference thereto. This reference more specifically defines the formula to predict oil droplet size and the formula for the Weber Number, including each of the variables in the respective formulas and the manner of determining each.

As was previously indicated, alternatively to separating the oil droplets from the oil-in-water emulsion(s), the existing oil-in-water emulsion(s) can be used in its existing state for fuel, and there would be no necessary in separating the oil droplets from the existing oil-in-water emulsion(s). In instances where the oil-in-water emulsion(s) is to be burned as fuel, it is sent or fed directly into any suitable boiler means for combustion. The boiler means may be any conventional boiler (e.g., a fluidized bed boiler, a marine boiler, a power plant boiler, etc.) or combustion apparatus wherein fuel (e.g., the oil-in-water emulsion(s)) is burned for any suitable purpose, such as to produce steam from water that is to be evaporated within coils heated by the boiler, etc.

In many instances the produced or otherwise available hydrocarbon (i.e., crude oil, bitumens, tars, resids, etc.) contains high levels of contaminants or obnoxious elements, such as sulfur, nitrogen, and metal (e.g., nickel, vanadium, etc.) containing compounds, etc. When such contaminated hydrocarbons are to be employed as fuels for boilers, or any other combustion process, the contaminants or obnoxious elements have to be removed from the fuel prior to combustion or from the combustion flue gases after combustion for the combustion process to be environmentally acceptable. The necessity for removing contaminants affects the economics of the combustion process. Existing utility plant or boiler technology employed for burning high sulfur-type fuels in an environmentally acceptable manner is limited and expensive with respect to investment and operating costs. Stack gas desulfurization technology and fluid bed combustion are primarily limited to major utility plants, and have not been fully accepted by industry. Contaminated hydrocarbons containing high levels of sulfur (e.g., 1 wt. % to 8 wt. %), such as the majority of crude oils existing in Canada and Venezuela, have limited use as fuel and must be desulfurized first, an expensive operation. Thus, what is needed and what has been invented is an economical process for removing and/or reducing the emissions of contaminants or obnoxious elements from the combination of produced or otherwise available hydrocarbons, such as crude oil, bitumens, tars, resids, etc. More particularly as to what is needed and what has been invented is an economically and environmentally acceptable combustion process which includes the removal of contaminants or obnoxious elements. The process(es) is ideally suited for contaminated hydrocarbons broadly comprising from about 0.01 wt. % to about 8.0 wt. % of the contaminants and/or obnoxious elements, more specifically for contaminated hydrocarbons more narrowly comprising 0.40 wt. % to about 3.0 wt. %. By "contaminants" and/or "obnoxious elements" is meant any undesirable, economically and/or environmentally unacceptable constituent(s) within the contaminated hydrocarbon including, but not limited to, sulfur and/or sulfur containing compounds; nitrogen and/or nitrogen containing compounds; metals (e.g., nickel, vanadium, copper, etc.) and/or compounds containing metals; and etc.

The process(es) for removing contaminants broadly comprises mixing, commingling, or otherwise admixing, the emulsifying composition(s) and/or the hydrocarbon with a reactant or catalyst or the like (hereinafter referred to as "reactant") which reacts with or otherwise removes the contaminants from the hydrocarbon prior to or during the combustion process, provided that an oil-in-water emulsion(s) is formed containing the hydrocarbon as oil droplets, preferably having a particle size ranging from about 1.mu. (i.e., 1 micron) to about 200.mu., more preferably from about 10.mu. to about 100.mu.. The small particle size of the oil droplets provides a large reactive surface exposed to the reactant to facilitate the removal of contaminants from the hydrocarbon. Furthermore, when the oil-in-water emulsion(s) is to be introduced directly into a boiler for combustion, the small particle size of the oil droplets provides a large reactive surface exposed to combustion such that more heat is developed in the combustion process due to improved combustion efficiency. The reactant may be any appropriate compound, element, or the like, in the emulsifying composition(s) and/or hydrocarbon which will combine with, react with, or promote the reaction of the contaminants within the hydrocarbons to form a gas or particulate which can be recovered or captured, either directly from the oil-in-water emulsion before combustion or subsequent to combustion of the oil-in-water emulsion all of which will be explained below in greater detail. The reactants contained within the captured or recovered gas or particulate may be treated, separated or removed therefrom such that the contaminant component may be sold or otherwise disposed, and the removed reactant is regenerated and can be recycled for admixing with the emulsifying composition(s) and/or the hydrocarbon. Combustion of the oil-in-water emulsion(s) produces hot combustion gases which can be used for any suitable purpose, such as to produce steam.

In a preferred embodiment of the invention, the reactant(s) may be any suitable aqueous phase (water) soluble reactant(s), hydrocarbon (oil) soluble reactant(s), or insoluble (i.e., insoluble in both aqueous phase and hydrocarbon phase) reactant(s), or mixtures of any of the foregoing reactant(s). Suitable aqueous phase soluble reactant(s) may include, but are not limited to, any of the following, or mixtures of any of the following, reactants: slaked lime, Ca(OH).sub.2 ; sodium carbonate, Na.sub.2 CO.sub.3 ; sodium bicarbonate, NaHCO.sub.3 ; sodium hydroxide, NaOH; sodium acetate, NaCH.sub.3 COO; potassium carbonate, K.sub.2 CO.sub.3 ; potassium bicarbonate, KHCO.sub.3 ; potassium hydroxide, KOH; potassium acetate, KCH.sub.3 COO; calcium bicarbonate, Ca(HCO.sub.3).sub.2 ; calcium acetate, Ca(CH.sub.3 COO).sub.2 ; magnesium hydroxide, Mg(OH).sub.2 ; magnesium acetate, Mg(CH.sub.3 COO).sub.2 ; magnesium bicarbonate, Mg(HCO.sub.3).sub. 2; aluminum acetate, Al(CH.sub.3 COO).sub.3 ; sodium aluminate, NaAlO.sub.2 ; potassium aluminate, KAlO.sub.2 ; and sodium stearate. More preferably, the aqueous phase reactant(s) is selected from the group consisting of slaked lime (Ca(OH).sub.2), sodium carbonate (Na.sub.2 CO.sub.3), sodium hydroxide (NaOH), and mixtures thereof. The most preferred aqueous phase reactant is slaked lime (Ca(OH).sub.2). The preferred hydrocarbon (oil) soluble reactant(s) is selected from the group consisting of calcium naphthenate; sodium dinonyl naphthalene disulfonate; and calcium stearate; and mixtures thereof. The insoluble reactant(s) for a preferred embodiment of the invention is selected from the group consisting of calcium carbonate (limestone), CaCO.sub.3 ; calcium-magnesium carbonates (dolomites); aluminum oxide, Al.sub.2 O.sub.3 ; aluminum hydroxide, Al(OH).sub.3 ; aluminum carbonate, Al.sub.2 (CO.sub. 3).sub.3 ; magnesium carbonate, MgCO.sub.3 ; magnesium oxide, MgO; iron oxides, FeO, Fe.sub.2 O.sub.3, Fe.sub.3 O.sub.4 ; and iron carbonates, FeCO.sub.3, Fe.sub.2 (CO.sub.3).sub.3 ; and mixtures thereof. More preferably, the insoluble reactant(s) is magnesium carbonate (MgCO.sub.3), calcium carbonate (limestone, CaCO.sub.3), and calcium-magnesium carbonates (dolomites), and mixtures thereof; most preferably calcium carbonate (limestone, CaCO.sub.3), and calcium-magnesium carbonates (dolomites), and mixtures thereof. When any of the reactant(s) are in solid form, they are typically granulated or ground into small particle sizes, for example particulate matter ranging from 0.1.mu. to 500.mu. in size with 1.mu. to 100.mu. being more preferable, before mixing with the emulsifying composition(s) and/or the hydrocarbon.

The emulsifying agent(s) may be any emulsifying agent which is compatible with the reactant(s) that is to be added to the hydrocarbon and/or emulsifying composition(s) and which, when combined with an appropriate quantity of aqueous phase, is capable of initially forming the emulsifying composition(s) and subsequently forming in the hydrocarbon during or after agitation (i.e., either dynamic or static) an oil-in-aqueous phase emulsion wherein the reactant(s) either before, during, or after combustion will combine with, react with, or promote the reaction or otherwise removal of any contaminants contained in the hydrocarbon to form a gas or particulate which as previously indicated, can be preferably recovered or captured. The emulsifying agent(s) may be anionic, cationic, nonionic, amphoteric, and the like. Preferably, the emulsifying agent(s) is either anionic and/or nonionic, with nonionics being presently preferred because they are not affected by the reactant(s) and/or the contaminants contained within the hydrocarbon and because they are generally cheaper. Most preferably, the emulsifying agent(s) is any of the previously mentioned emulsifying agent(s) of this invention including, but not limited to, the following: [A] those emulsifying agent(s) selected from the compounds having general formulas (1) and (2) as further described above; [B] those emulsifying agents selected from the compounds having general formulas (3) and/or (4) as further described above; [C] those emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 1966 to about 9188, and the above stated general formula: ##STR20## wherein n.sub.1 is an integer and has a value of from about 7 to about 20, preferably 11, and y.sub.1 is an integer having a value of from about 4 to about 1000; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188; and wherein the emulsifying agent(s) has at least one ethoxylated alkylphenol compound having the above stated general formula: ##STR21## wherein n.sub.1 has a value of from about 7 to about 20, preferably 11; and y.sub.1 is greater than 100, preferably greater than 100 but less than 1000, and the ethoxylated alkylphenol compound of general formula (5A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s); [D] those emulsifying agent(s) selected from the ethoxylated dialkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 2519 to about 11,627, and the above stated general formula: ##STR22## wherein n.sub.1 is an integer and has a value of from about 7 to about 18, n.sub.2 is an integer and has a value of from about 7 to about 18, and y.sub.2 is an integer having a value of from about 4 to about 1000; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627; and wherein the emulsifying agent(s) has at least one ethoxylated dialkylphenol compound having the above stated general formula: ##STR23## wherein n.sub.1 has a value of from about 7 to about 18, n.sub.2 has a value of from about 7 to about 18, and y.sub.2 is greater than 100, preferably greater than 100 but less than 1000; and the ethoxylated dialkylphenol compound of general formula (6A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s); [E] those emulsifying agent(s) selected from the ethoxylated alkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 558 to about 2504, and the above stated general formula: ##STR24## wherein n.sub.1 is an integer and has a value of from about 7 to about 14, preferably 8, and y.sub.1 is an integer having a value of from about 4 to about 200; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 558 to about 2504; and wherein the emulsifying agent(s) has at least one ethoxylated alkylphenol compound having the above stated general formula: ##STR25## wherein n.sub.1 has a value of from about 7 to about 14, preferably 8; and y.sub.1 is greater than 100, preferably greater than 100 but less than 200, and the ethoxylated alkylphenol compound of general formula (7A) preferably comprises at least about 1% by weight (more preferably from about 1% to about 10% by weight) of the emulsifying agent(s); [F] the emulsifying agent(s) being a combination of the ethoxylated alkylphenol compounds having the general formula (7) and emulsifying agent(s) selected from the ethoxylated alkyl compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular Weight of from about 2458 to about 4218, and the above stated general formula: ##STR26## wherein n.sub.1 is an integer and has a value of from about 9 to about 14, preferably 11, and y.sub.1 is an integer having a value of from about 4 to about 300; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 2458 to about 4218 and wherein the emulsifying agent(s) represented by general formula (8) has at least one ethoxylated alkylphenol compound having the above stated general formula: ##STR27## wherein n.sub.1 has a value of from about 9 to about 14, preferably 11; and y.sub.1 is greater than 100, preferably greater than 100 but less than 300, and the ethoxylated alkylphenol compound of general formula (8A) preferably comprises at least about 1% by weight (more preferably from about 1% to about 75% by weight) of the emulsifying agent(s); [G] those emulsifying agent(s) comprising about 50 percent by weight of an ethoxylated nonylphenol compound having the formula: ##STR28## wherein y.sub.1 is equal to 40 and is the average number of ethylene oxide units in the formula and about 50 percent by weight of an ethoxylated nonylphenol compound having the formula: ##STR29## wherein y.sub.2 is equal to 100 and is the average number of ethylene oxide units in the formula; [H] those emulsifying agents comprising at least one ethoxylated dialkylphenol compound having the general formula: ##STR30## wherein n.sub.1 is an integer having a value of from about 7 to about 18 and n.sub.2 is an integer having a value of from about 7 to about 18 and y.sub.1 is an integer having a value of from greater than 100 to about 250; and an ethoxylated alkylphenol compound selected from the group of ethoxylated alkylphenol compounds having the general formulas: ##STR31## and mixtures thereof, wherein y.sub.2 is an integer ranging from about 4 to about 100, y.sub.3 is an integer ranging from about 4 to about 100, and R.sub.1, R.sub.2 and R.sub.3 are each an alkyl radical containing from about 8 to about 21 carbon atoms; and [I] those emulsifying agents comprising at least one ethoxylated alkylphenol compound having the general formula: ##STR32## wherein n.sub.1 is an integer having a value of from about 7 to about 20 and y.sub.1 is an integer having a value of from greater than 100 to about 250; and an ethoxylated alkylphenol compound selected from the group of ethoxylated alkylphenol compounds having the general formulas: ##STR33## and mixtures thereof, wherein y.sub.2 is an integer ranging from about 4 to about 100, y.sub.3 is an integer ranging from about 4 to about 100, and R.sub.1, R.sub.2 and R.sub.3 are each an alkyl radical containing from about 8 to about 21 carbon atoms.

The quantity or amount of reactant that is to be supplied to the emulsifying composition(s) and/or the hydrocarbon to react with (or otherwise remove) contaminants is a substantially stoichiometric amount, or slightly more than the stoichiometric amount, for example 1 to 35% by wt., more preferably about 25% by wt., in excess over the stoichiometric amount. Thus, if a given quantity of contaminated hydrocarbon contains from about 0.01 wt. % to about 8.0 wt. % contaminants, then the quantity or amount of reactant that is to be added to the emulsifying composition(s) and/or to the contaminated hydrocarbon is from about 1 to 35% by wt. in excess of the required weight of the reactant to react with 0.01 wt. % of contaminant to about 1 to 35% by wt. in excess of the required weight of the reactant to react with 8.0 wt. % of contaminant. By way of example only, if 100 lbs. of hydrocarbon fuel oil contains 1 wt. % S, and slaked lime (Ca(OH).sub.2) is to be the reactant (or sorbent additive) with a 25 wt. % stoichiometric excess, the quantity (with 25 wt. % in excess) of lime reactant to be used with the 100 lbs. of hydrocarbon fuel oil would be 1 lb. S (2.31 lb. Ca(OH).sub.2 /lb. S).times.(1.25), or 2.89 lbs. The typical oil-in-water emulsion composition with the lime reactant would be 100 lbs. hydrocarbon fuel oil (68 wt. %), 44.1 lbs. of emulsifying composition(s) (30 wt. %), and 2.89 lbs. of lime reactant (1.0 wt. %). As was previously indicated, any reactant would be added directly to the emulsifying composition(s) and/or hydrocarbon. Therefore, the 2.89 lbs. of lime reactant could be added directly to the 44.1 lbs. of emulsifying composition(s) or to the 100 lbs. of hydrocarbon fuel oil, or divided between the 44.1 lbs. of emulsifying composition(s) and the 100 lbs. of hydrocarbon fuel oil.

By way of further example only: If 100 lbs. of hydrocarbon fuel oil is contaminated with 0.01 to 8.0 wt. % of sulfur, and aluminum oxide (Al.sub.2 O.sub.3) and sodium stearate and calcium carbonate (limestone, CaCO.sub.3) are independently employed as the reactant with a 25 wt. % stoichiometric excess, the quantity (with 25 wt. % in excess) of each reactant per 100 lbs. of hydrocarbon fuel oil that would be used for 0.01 wt. % sulfur is: 0.01 lbs. of Al.sub.2 O.sub.3, 0.24 lbs. of sodium stearate, and 0.04 lbs. of CaCO.sub.3. For 8.0 wt. % sulfur, the quantity (with 25 wt. % in excess) of reactant per 100 lbs. of hydrocarbon fuel oil that would be used is: 10.6 lbs. Al.sub.2 O.sub.3, 191.2 lbs. of sodium stearate, and 31.2 lbs. of CaCO.sub.3. The exact quantity of each reactant would depend on the exact amount of sulfur in the contaminated hydrocarbon fuel oil. Since the quantity range of sulfur in the contaminated hydrocarbon fuel oil is 0.01 to 8.0 wt. %, the quantity range of each reactant that would be added to the emulsifying composition(s) and/or the hydrocarbon fuel oil would range from 0.01 to 10.6 lbs. for sodium stearate, and 0.04 to 31.2 lbs. for CaCO.sub.3. Thus, if the 100 lbs. of hydrocarbon fuel oil is contaminated with 1.0 wt. % sulfur, either 1.32 lbs. of Al.sub.2 O.sub.3 or 23.9 lbs. of sodium stearate or 3.9 lbs. of CaCO.sub.3 could be employed as the reactant.

After the appropriate quantity of reactant has been admixed with the emulsifying composition:,s) and/or hydrocarbon, the contaminated hydrocarbon is agitated (e.g., dynamically and/or statically) with the emulsifying composition(s), preferably at a temperature of 80.degree. F. to 212.degree. F., or 213.degree. F. to 250.degree. F. under pressure and immediately quenching to a temperature of 150.degree. F. or less, to form an oil-in-aqueous phase emulsion(s), wherein the amount of aqueous phase in the oil-in-aqueous phase emulsion(s) is from about 10% to about 70% by weight and wherein the emulsifying agent(s) used is an amount sufficient to assist in the formation of the oil-in-aqueous phase emulsion(s). The reactant may be added to the emulsifying composition(s) on the surface of the earth, and the emulsifying composition(s) containing the reactant can be injected downhole to contact and mix with contaminated hydrocarbon to form the oil-in-aqueous phase emulsion(s) at any desired location in accordance with any of the previously mentioned procedures (e.g., formation of oil-in-aqueous phase emulsion(s) downhole or within the subterranean reservoir itself, etc.). Similarly, the reactant (including a suitable compatible carrier such as water, etc.) can be injected downhole directly to mix with the contaminated hydrocarbon and forming the oil-in-aqueous phase emulsion with the emulsifying composition(s) mixing/contacting the contaminated hydrocarbon containing the reactant. Mixing of the reactant with the contaminated hydrocarbon would be either downhole as the contaminated hydrocarbon immediately produced from the reservoir or within the subterranean reservoir itself which contains the contaminated hydrocarbon.

As was previously indicated, during and/or after the formation of the oil-in-aqueous phase emulsion(s), the reactant reacts with or adsorbs or otherwise removes the contaminates as gas or particulates from the contaminated hydrocarbon, which is in the form of oil droplets in the oil-in-aqueous phase emulsion. Subsequent to forming the oil-in-aqueous phase emulsion and with the latter being available (such as on the surface of the earth), the oil-in-aqueous emulsion may be further processed as desired, such as for pipeline transportation or for combustion. It should be understood that the reactant(s) may be of the type that functions prior to or concurrent with the combustion process. For example, an oil-in-aqueous phase emulsion prepared for the purpose of transporting a heavy hydrocarbon can include reactant(s) in the aqueous phase which extract undesirable components from the contaminated hydrocarbon during the transportation process.

In a preferred embodiment of the invention, the oil-in-aqueous phase emulsion containing the contaminants is introduced directly into a boiler/furnace for combustion purposes. As previously indicated, the boiler/furnace may be any suitable boiler or furnace means, but is preferably a conventional dispersed-fuel boiler or a fluidized bed boiler. For combustion with a dispersed-fuel boiler, the oil-in-aqueous phase emulsion is sprayed into the combustion chamber in combination with combustion air. Usually steam atomization, air atomization or mechanical atomization are employed in fuel-fired boilers for combustion of pure fuel oil and would be similarly employed in the present invention to atomize the oil-in-aqueous phase emulsion into particle size ranging from 1.mu. to about 400.mu., preferably 10.mu. to 100.mu., albeit the nozzle configuration and atomizing fluid rates may be adjusted to conform to the viscosity of the oil-in-aqueous phase emulsion. Steam is raised by exposure of boiler tubes containing boiler feed water, to the flowing hot combustion gases and the consequent exchange of heat into the water. Conventional steam raising and control equipment is preferably used in the present invention of oil-in-aqueous phase emulsion combustion, in like manner to the combustion of fuel oil. Soot blowers are commonly, but not universally, employed in fuel oil fired boilers to periodically clear accumulated particulates away from boiler tubes, thereby maintaining high heat transfer efficiency of the boiler tubes. For the application of the present invention using oil-in-aqueous phase emulsions with sulfur-absorbent additives, soot blowers may be required in order to avoid a decline in boiler performance due to dust accumulation on the tubes. Particulates formed in the combustion process are predominantly entrained in the combustion gases through the boiler section and can be removed from the partially cooled gases by common equipment such as settling chambers, centrifugal (cyclone) dust separators, electrostatic precipitators and baghouses (fabric filters). Such means of dust removal are commonly employed in fuel oil fired boilers and furnaces for burning pure fuel oil, and would be similarly used in the application of oil-in-aqueous phase combustion. However, when additives are used for sulfur capture, the dust loading will typically be higher than in pure fuel oil combustion.

In a conventional fluidized-bed boiler the fuel and air are dispersed into an agitated bed of hot solid particulates, usually comprised of a sulfur sorbent, ash and unburned carbon. The combustion process occurs within the fluidized bed and sulfur oxides released by fuel oxidation are absorbed by any sulfur sorbent present in the fluidized bed. Sorbent must be fed to the fluidized bed on a continuous or periodic batch basis and spent sorbent removed likewise. In the application oil-in-aqueous phase combustion the sorbent may be admitted to the fluidized bed with the oil-in-aqueous phase emulsion or separately, as is common practice with firing of fuel oil. Steam is raised by means currently employed in the industry, and similar to the means used in conventional boilers, with the exception that boiler tubes are usually present in the fluidized bed of solids, where heat transfer rates are relatively high. Boiler tubes are also placed in the effluent gas stream, similar to conventional boilers. Particulate systems for fluidized bed boilers typically employ the same common equipment types used in conventional boilers. Cyclone separators are commonly used to return a major portion of the particulates to the fluidized bed. Further cleaning of the effluent gas usually employs electrostatic precipitation and/or baghouses.

As was previously indicated, the reactant(s) from captured particulates containing contaminants may be removed or separated therefrom and recycled for admixing with the emulsifying composition(s) and/or hydrocarbons. For example, reactant MgO in an oil-in-aqueous phase emulsion containing hydrocarbon contaminated with S reacts with and removes the S by forming MgSO.sub.3 or Mg(HSO.sub.3).sub.2 in sorbing the SO.sub.2 it contacts. MgO may be regenerated from these species by calcining at 1500.degree. F. More particularly by way of example only and not by limitation, 100 lbs. of contaminated hydrocarbon fuel oil having 1 lb. of S is agitated with an emulsifying composition(s) containing 1.56 lbs. MgO supplied as absorbent with 25 wt. % stoichiometric excess [i.e., 1 lb. S (1.25 lbs. MgO/lb. S) (1.25 excess)=1.56 lbs.]. The composition of oil-in-aqueous phase emulsion is 100 lbs. of contaminated hydrocarbon fuel oil (68.9 wt. %), 1.56 lbs. of reactant MgO (1.1 wt. %), and 43.5 lbs. of emulsifying composition (30.0 wt. %). Assuming that 100% of sulfur is captured as Mg(HSO.sub.3).sub.2, the total weight of Mg(HSO.sub.3).sub.2 would be 5.81 lbs. [i.e., 1.25 lbs. MgO (186 lbs. Mg(HSO.sub.3).sub.2 /40 lbs. MgO=5.81 lbs.]. Unreacted MgO is equal to 1.56 lbs.-1.25 lbs. or 0.31 1bs. MgO. Mg(HSO.sub.3).sub.2 would be reacted with MgO to form MgSO.sub.3 by the formula: Mg(HSO.sub.3).sub.2 +MgO+11 H.sub.2 O.fwdarw.2MgSO.sub.3 .multidot.6 H.sub.2 O. The next MgO to be added to the spent reactant is 0.94 lbs. [i.e., 1.25 lbs. (added MgO required) less 0.31 lbs. (unreacted MgO already present)]. The quantity of MgSO.sub.3 formed is 6.5 lbs. [i.e., 2(1.25 lbs. MgO)(104 lbs. MgSO.sub.3 /40 lbs. MgO)=6.5 lbs. MgSO.sub.3 ]. The MgSO.sub.3 is calcined to MgO at 1500.degree. F. by the formula MgSO.sub.3 .multidot.6 H.sub.2 O.fwdarw.MgO+SO.sub.2 +6 H.sub.2 O. When 13.25 lbs. of MgSO.sub.3 .multidot.6 H.sub.2 O [i.e., 6.5 lbs. MgSO.sub.3 (212 lbs. MgSO.sub.3 .multidot.6 H.sub.2 O/104 lbs. MgSO.sub.3)=13.25 lbs. MgSO.sub.3 .multidot.6 H.sub.2 O] is fed to a calciner, 2.5 lbs. of MgO [i.e., 13.25 lbs. MgSO.sub.3 .multidot.6 H.sub.2 O (40 lbs. MgO/212 lbs. MgSO.sub.3 .multidot.6 H.sub.2 O) =2.5 lbs. MgO] is formed for recycle to be admixed with the emulsifying composition(s) and/or contaminated hydrocarbon, or for recycling to the combustion and/or to the regenerator.

In another preferred embodiment of the present invention, the undesirable contaminants within the contaminated hydrocarbon are extracted into the aqueous phase by reactants known as chelates. One advantage of a dispersed contaminated hydrocarbon phase within a continuous aqueous phase is the large interfacial area residing between the two fluids. This large interfacial area provides the accessibility to the natural contaminating components in the hydrocarbon phase for extraction into the aqueous phase. The chelating agents would be preferably employed to extract and remove the contaminants from the contaminated hydrocarbon prior to combustion in order to improve the efficiency of the combustion process and also remove inorganic contaminants that would exist in the combustion products resulting from the combustion process. A low-cost mechanism employing chelates for removing contaminants from contaminated hydrocarbon dispersed in an aqueous phase is solvent extraction well publicized in the literature.

K. Osseo-Asare of the Department of Materials Science and Engineering, the Pennsylvania State University, in an article entitled "Interfacial versus Aqueous Phase Reactor Sites in the Solvent Extraction of Metal Ions: The Ambiguity of Correlation Plots" published in Colloids and Surfaces, 33 (1988) 209-215, describes how solvent extraction processes, particularly those involving chelating reagents and metal ions, can in principle be controlled by mass transfer processes or chemical reactions or combinations of these. K. Osseo-Asare more particularly describes that when the adsorption density of the extractant is below its saturation value, the adsorption density and the distribution coefficient of the extraction reagent are interrelated in such a way that in terms of the relevant mathematical expressions, an interfacial reaction can mimic a bulk aqueous phase reaction and vice versa. Douglas S. Flett of Warren Spring Laboratory, Stevenage, Herts, United Kingdom, in an article entitled "Chemical Kinetics of Copper Chelates"published in Solvent Extraction (Vol. 10, 1977) discusses the chemical kinetics and mechanism of metal extraction with certain chelating extracts, such as 2-hydroxy-5-nonylbenzophenone oxime (the active extractant in the commercial reagent LIX 65N sold by General Mills Inc.). Other suitable commercial reagents were shown by Flett to include those sold under the trade name LIX 63, LIX 70 (both by General Mills Inc.), SME 529 by Shell Chemicals Ltd. U.K., P. 17 and P 50 by Acorga Ltd. U.K., and Kelex 100 by Ashland Chemical Co. U.S.A. Wasan et al. in "Separation of Metal Ions by Ligand-accelerated Transfer through Liquid Surfactant Membranes", published in Faraday Discuss. Chem. Soc. (1984, 77, 67-74), describes that the rate of extraction of heavy-metal ions is greatly accelerated by the presence of a ligand in the aqueous solution containing the metal ions. The ligand effect on interfacial mass-transfer rates was defined by Wasan et al. by measuring the rate of extraction of cobalt by di-2-ethylhexyl phosphoric acid using sodium acetate as ligand in a modified Lewis cell. The effect of a surfactant such as polyamine on mass transfer at liquid/liquid interfaces was investigated and was found to be quite significant. Other articles appearing in Faraday Discuss. Chem. Soc. (1984), 77) were (on pages 189-196) "The Contribution of Chemistry to New Marangoni Mass-transfer Instabilities at the Oil/Water Interface" by Nakache et al. which discusses the spontaneous interfacial motions appearing at an interface between two immiscible phases in a state far from equilibrium (e.g., an aqueous phase of an organic acid or a complex ion and an organic phase of a long-chain surfactant molecule); and (on pages 209-216) "Transfer of Alkali-metal and Hydrogen Ions across Liquid/Liquid Interfaces Modiated by Monensin" by Koryta et al. which describes that under certain conditions the interface between an aqueous phase and an organic phase (ITIES, interface of two immiscible electrolyte solutions) has certain properties analogous to a metal/electrolyte-solution interface, and that by polarization of the ITIES using potential-sweep voltammetry, reproducible voltammograms corresponding to ion transfer across the ITIES are obtained. Koryta et al. further describes that in the presence of cation-complexing ionophores in the organic phase, cation transfer is facilitated, and the acidic form HX of carboxylic ionophores, monensin A and B, acts in the nitrobenzene/water system as a sodium carrier while the complex of its anion with sodium or lithium cation (M.sup.+) is a proton carrier. Hamabusa Michio in JP 63, 158, 123, Jul. 1, 1988 (Appl. 86/305, 369, 23 Dec. 1986) describes the use of a chelating agent (i.e., an Fe ion-chelating agent) in an oil-in-aqueous phase emulsion that was combusted in a boiler, resulting in the decrease of soot formation and the increase of combustion efficiency by 80% or higher than by the use of emulsifying agents alone.

Another low-cost extraction method for removing contaminants from contaminated hydrocarbon removes certain low molecular weight organic compounds from the contaminated hydrocarbon by the existence of the so-called "emulsion liquid membrane" that already resides at the oil/water interface. Separation processes based on emulsion liquid membranes was first developed by Norman N. Li, as described in U.S. Pat. No. 3,410,794 to Li which is incorporated herein by reference. Wiencek et al. in an article entitled "Solubilization in Microemulsions and Application to Separations" (published in Colloids and Surfaces, 29 (1988), pages 199-131) discusses a new class of separation techniques employing liquid membranes based on microemulsions rather than coarse emulsions. Tondre et al. published an article in Faraday Discuss. Chem. Soc. (1984, 77, pages 115-126) entitled "Use of Microemulsions as Liquid Membranes" wherein water-in-oil microemulsions composed of decane, water, tetraethyleneglycol dodecylether (TEGDE) and hexan-1-ol were used as liquid membranes and the microglobules were shown to transport alkali-metal picrates between the two aqueous phases.

In a more preferred embodiment of the present invention the reactant-contaminants or the chelate complexes (which include the contaminants removed from the contaminated hydrocarbon) are removed from the oil-in-aqueous phase emulsion prior to combustion. Separation and removal of the contaminants from the aqueous phase can be by any suitable means such as the gravitational pulling described in "Simultaneous Treatment of Crude Oil Containing Iron and Sulfur" (USSR SU 1,414,859), accelerated settling and separation by the use of flocculants as in "Selected Organic Polymers for the Selective Flocculation of Titanium and Iron Ores" (Eur. Pat. Appl. EP 232,679), and conventional separators to accelerate and enhance separation by centrifugal means (cyclones, centrifuges, vortices, etc.).

Thus, by practice of another embodiment of the present invention there is provided a method for forming an oil-in-aqueous phase emulsion by agitating a contaminated hydrocarbon with an emulsifying composition(s) wherein a reactant and/or chelating agent has been previously mixed with the contaminated hydrocarbon and/or emulsifying composition(s) or mixed during the agitation of the contaminated hydrocarbon and emulsifying composition(s), while simultaneously causing or causing upon combustion the contaminants to be removed from the contaminated hydrocarbon which is in the form of droplets within the oil-in-aqueous phase emulsion. The concept can be used for disposal of pesticides or environmental hazardous chemicals and wastes, or used in combination with shale oil for combustion in a fluidized bed unit or reactor. Coal or other carbonaceous material in a pulverized state having an average particle size of less than 400 microns (preferably less than 200 microns) can be added to either the hydrocarbon phase and/or to the emulsifying composition(s) phase and/or to the oil-in-aqueous phase; or the coal or other carbonaceous material in the pulverized state alone (with no other hydrocarbon employed) may be used with the emulsifying composition(s) of this invention to formulate a coal-in-aqueous phase emulsion, or a slurry comprising the particulate coal or carbonaceous material suspended in the emulsifying composition(s).

Any of the foregoing, previously mentioned emulsifying agent(s) and/or emulsifying compositions(s) of this invention may be employed to form a coal-in-aqueous phase slurry or mixture, especially for pipeline transporting purposes.

Any of a wide variety of coals can be used to form the coal-in-aqueous phase mixtures of the present invention, including anthracite, bituminous, sub-bituminous, mine tailings, fines, lignite and the like. Other finely divided solid carbonaceous materials may also be used, e.g., coke, prepared either from coal or from petroleum. Thus, whenever "coal" is used herein, it is to mean any particulate carbonaceous matter, including but not limited to carbon, coke, any of the various types of coal, etc. The coal has to be pulverized or particulated to a suitable size, preferably to an average particle size less than 200 microns, or alternatively, from 40% to 95% finer than a 200 mesh Tyler Standard screen size, although coarser or finer particle sizes can be employed if desired.

The untreated pulverized raw coal is preferably beneficiated, i.e., cleaned of amounts of ash and sulfur or other undesirable constituents. Those skilled in the art will appreciate that mixtures formed of beneficiated coal offer considerable advantage. They are clean burning or relatively clean burning, and are more suited for burning in apparatus for powering utilities, home burners and the like without undue burdensome and expensive cleaning apparatus.

There are a wide array of beneficiating treatments which can be employed in preparing the particulate coals, including conventional heavy-media separations, magnetic separation and the like. The preferred method for providing the beneficiated coal particles is by a chemical treatment process such as that described in U.S. Pat. No. 4,304,573. As was previously indicated, the previously described reactants (including chelating agents) can be employed as a beneficiator. U.S. Pat. No. 4,304,573 is fully incorporated herein by reference thereto.

Generally, according to the preferred chemical beneficiation treatment method, raw as-mined coal is ground in the presence of water to a particle size of about 200 mesh. The ground coal is treated in an aqueous medium with a monomeric compound, generally an unsaturated polymerizable composition such as readily available tall oil fatty acids in the presence of a metal initiator such as cupric nitrate; and minor amounts of fuel oil, all in an aqueous phase are also present. The ground coal so treated is made hydrophobic and oleophilic and is separated from the unwanted ash and sulfur by a froth flotation technique.

The cleaned coal recovered from the preferred chemical treatment process, now in the form of beneficiated coal particles, is suited for the coal-in-aqueous mixtures of the present invention. These coal particles are characterized by having an ash content reduced to levels of about 0.5 to 6.0% and a sulfur content reduced to levels of about 0.5 to 2.0%.

In a preferred embodiment of the present invention, the coal-in-aqueous phase mixture of the present invention may be formed by first adding any of the emulsifying agent(s) of this invention to the aqueous medium together with other additives such as conventional defoaming agents, if desired. This admixing can be done with stirring at conditions of atmospheric or nearly atmospheric temperature and pressure. Thereafter, the particulate coal, preferably beneficiated coal particles, is added to the mixture to produce a coal-in-aqueous phase mixture of coal solids content of from about 10 to 80% by weight coal, based on the total weight of the mixture at atmospheric or nearly atmospheric temperatures and pressures. If desired, thickeners can then be added to further stabilize the mixture to assist in preventing the coal particles from settling when the mixture is to be stored for extended periods. Caustic soda or other bases can also be added at this point. As will be apparent, adding thickeners in or near the final stage is preferred so that any stirring requirements are kept at a minimum. The coal-in-aqueous phase mixtures of this invention can be prepared in a batch operation or in the continuous mode. In continuous production, the coal can be admixed with water in a first stage along with other flow control agents such as the surfactant. The compositions of the first stage can then be transferred continuously to a second stage wherein the thickener is added. Again adding the thickener at the later stage results in reduced stirring requirements.

Mixing and dispersing apparatus(es) which can be employed in the present invention may be any suitable type, such as premier Mill Co.'s Hi-Vispersator High-Speed Disperser. In the formulation of the coal-in-aqueous phase mixtures of the present invention with any suitable mixer-apparatus, residence times, temperatures, mixing speeds, etc. may vary according to specific process requirements such as the volume of ingredients, size of apparatus, mixing efficiency, etc. Thus, for example, depending on the scale of the operation, e.g. pilot plant, plant, etc., these process parameters may be adjusted accordingly. When suitable process parameters are employed, the coal is allowed to be dispersed in a surfactant/antifoam solution at relatively low viscosity, while the surfactant is orienting at the coal-water interface. The anti-foam agent controls the level of foam caused by the surfactant being agitated in solution. The thickeners are added after the coal is adequately dispersed to impart the desired rheological and suspension properties from flocculating by forming a protective colloid.

As was previously indicated, additives that can be added to the coal-in-aqueous mixture include defoaming agents, thickeners, salts, bases, other flow modifying agents and combinations of these materials.

Generally, the defoaming agents that can be used are conventional and include both silicon and nonsilicon containing compositions. A commercially available defoaming agent suitable for use in the mixture is a defoaming agent sold under the trademark COLLOID 691.RTM. by Colloids, Inc. This composition generally comprises a mixture containing mineral oil, amide and an ester.

Any thickeners added to the coal-in-aqueous phase mixture increase the non-settling characteristics of the composition. Suitable thickeners include, for example, xanthan gum, guar gum, glue and the like. Other thickeners include, for example, alkali soluble acrylic polymers (e.g., commercial products sold under the registered trademark ACRYSOL ICS-L.RTM. by the Rohm and Haas Company). Combinations of these thickeners are also contemplated herein. For the purposes herein, the thickeners are generally used in amounts ranging from about 0.01 to about 3.0% by weight, based on the total weight of the mixture.

In preparing the coal-in-aqueous phase mixtures containing 50 to 70% by weight coal (preferably 60 to 70% by weight), based on the weight of the total mixture, the emulsifying agent(s) of the present invention are preferably mixed with the aqueous phase in a proportion of from about 0.1 part to about 0.3 part by weight emulsifying agent, from about 10.0 to about 30 parts by weight aqueous phase at atmospheric or nearly atmospheric temperatures and pressures. A defoaming agent can also be added to the aqueous phase in an amount of about 0.01 to about 0.03 part by weight, to assist in processing. The pulverized coal is then mixed with the aqueous phase in a proportion of 50 to 70 parts by weight coal to 10 to 30 parts by weight of aqueous phase to obtain a flowable solution or about 0.09 to about 0.15 part by weight of thickener or thickeners to provide protection against settling. Other additives such as salts or bases, antibacterial agents such as formaldehyde, and the like, viscosity stabilizers, such as ammonia, etc. can also be added in from about 0.1 to about 0.3 part by weight, of the total mixture to further assist in dispersing the coal and providing other obvious advantages. As was previously indicated, the transportable coal-in-aqueous phase mixture or slurry may be pipelined directly into a boiler means for coal/water fuel firing.

Coal-in-aqueous phase slurry viscosity depends on the type of surfactant used and on other formulation factors, as shown in TABLE A below. Generally, the lower molecular weight surfactants are more effective per pound in reducing viscosity than higher molecular weight surfactants. Use of xanthan biopolymer apparently decreased the slurry viscosity somewhat. This xanthan effect is unexpected as xanthan is known to increase the viscosity of oil-in-aqueous phase emulsions. Preferably, the quantity of biopolymer xanthan to be added varies from about 0.3 to about 1.5 parts by weight of xanthan, per part by weight of surfactant (or emulsifying agent(s)), with 1 part of xanthan to 1 part of surfactant being the more preferred.

It can be seen from TABLE A that the concentration of surfactant is quite important with regard to viscosity, with a major improvement seen in going from 1,000 ppm to 2,000 ppm. Thus, the use of higher surfactant concentrations would permit operation at higher coal/water ratios. It can be further seen that oil-in-aqueous phase fine particle size causes much higher slurry viscosity, as expected. The wide particle size distributions slurry (-100 mesh) exhibits lower viscosity than any of the narrow-cut slurries, similar to observations with oil-in-aqueous phase emulsions. Thus, the presence of fines in the coal is not detrimental unless fines concentration is excessive. Presence of fines in the slurry contributes to stability, inhibiting settling. Finally, the coal/water ratio has a drastic effect on slurry viscosity. Therefore, close control of this ratio is a major consideration in pipeline operation.

One of the salient features of the coal-in-aqueous phase mixture of the present invention is the redispersity of settled coal particulates, especially for certain of the emulsifying agent(s) of the present invention. By way of example only, redispersibility results are given in TABLE B below for -100 mesh coal. Generally, as can be seen from TABLE B below, the higher molecular weight surfactants provide better redispersibility, and there is advantage in going to higher surfactant concentration (note that surfactant concentrations reported with this test refer to the aqueous phase only as an excess of water phase must be used). Xanthan biopolymer in combination with the emulsifying agent(s) and/or emulsifying composition(s) of this invention improves redispersibility of the settled coal-in-aqueous phase slurry significantly. This is especially true for a 50/50 mixture of NP40/NP100, more particularly described in Example I below. Preferably, as indicated, xanthan is employed in a quantity ranging from about 0.3 to about 1.5 parts by weight of xanthan, per 1 part by weight of emulsifying agent(s) or surfactant(s), with a 1:1 ratio being more preferable.

Redispersibility capabilities, especially when the biopolymer xanthan is used, is important with respect to redispersing settled coat particulates. The coal-in-aqueous phase mixtures of this invention contain a particulate coal phase dispersed in an aqueous continuous phase. Dispersed particulate coal has a tendency to settle, especially when being transported through a long pipeline where a portion of the dispersed coal phase settles in the aqueous continuous phase to produce a mixture comprising a settled coal phase and a residual coal-in-aqueous phase mixture. The settled coal phase may be redispersed (e.g., by agitation or the like) into the residual coal-in-aqueous phase mixture. Alternatively to redispersing (through agitation) of the settled coal phase, additional aqueous phase may be added into the pipeline where settling has occurred. Such additional aqueous phase inherently has a diluting effect and a redispersing capability from injection pressure. After the addition of additional aqueous phase, the additional aqueous phase and the mixture comprising the settled coal phase and the residual coal-in-aqueous phase is transported through the pipeline. Additional emulsifying agent(s) and/or emulsifying composition(s), or emulsifying agent(s) and/or emulsifying composition(s) plus xanthan, may be added along the pipeline to the formed coal-in-aqueous phase mixture as it is being transported through the pipeline. Such addition retards the settling of particulate coal and allows the coal-in-aqueous phase mixture to be transported greater distances before being concerned with redispersibility.

Any of the foregoing, previously mentioned emulsifying agent(s) and/or emulsifying composition(s) of this invention may be employed with ultrasonic energy means to convert heavy hydrocarbons, crudes, and the like, into lighter products. The heavy hydrocarbon, asphaltenes, and the like, in their natural state exist in micelle form peptized with resin molecules. The center of the micelle can be either a metal, clay, water, or a combination. The essential feature is that polar groups are concentrated toward the center. It is postulated that this oil-external/water-internal (or reversed with oil being the internal and water the external) micelle (also known as monolamellar vesicles), when subjected to any suitable ultrasonic energy means, is exerted in a microenvironment to a location where it is utilized without heating the entire reactor volume. The conversion mechanism comprises (1) a rapid movement of fluids caused by variation of some pressure; (2) cavitation including the formation and collapse of microbubbles, where the pressure is estimated from theoretical considerations to be up to 75,000 psi or higher and the temperature is estimated to reach values up to 13,000.degree. F. or higher (note: this violent implosion of the microbubble also gives rise to lum escence); and (3) vibrational energy is put into small volumes with little heating. In a preferred embodiment of the invention, process of preparing a bilamellar vesicle or multimellar vesicle, such as, by way of example only, a water droplet or particle is surrounded by a hydrocarbon droplet or particle which in turn is surrounded by a water droplet or particle. The monolamellar or bilamellar vesicles carry free radicals such as hydrogen which, when activated, upgrades crude. The aqueous phase is admixed with a suitable catalyst (i.e., metal soluble cartalyst).

Hydrocarbon cracking reactions which occur at the locally elevated temperatures and pressures associated with exposure to ultrasonic energy may be promoted or catalyzed by compounds present in the hydrocarbon or in the free-water phase (or aqueous phase). These compounds may be added to the hydrocarbon or aqueous phase or they may be already present in the hydrocarbon. Catalysts, by way of example only, which may be added to the aqueous phase are as follows: Group 1: zinc chloride, ferrous sulfate, ferric chloride, cobalt nitrate, stannous chloride, cadmium acetate, cupric chloride, manganese nitrate, silver nitrate; Group 2: sulfuric acid, hydrochloric acid; Group 3: ammonium molybdate, ammonium vanadate. The species in Group 1 may be employed in alternate forms with anion substitution, as long as the compound is water soluble. For example, ferrous sulfate can be replaced with a substitute such as ferrous chloride or ferrous acetate. Metallic chlorides are particularly suited to promote asphaltene reactions.

Species from Group 2 are selected due to their acid character. Some species from Group 1, such as zinc chloride, exhibit acid behavior as well as cation activity, and this is beneficial.

Species from Group 3 exhibit activity from the metal, however the metal is soluble in water as part of the anion. A different cation may be substituted as long as water solubility remains and the cation does not suppress activity. For example, potassium molybdate might be substituted for ammonium molybdate.

Examples of species which may be added to the oil or hydrocarbon phase to promote reactions are as follows: cobalt naphthenate, nickel naphthenate, zinc naphthenate, tin naphthenate, iron naphthenate, copper naphthenate, cadmium naphthenate, manganese naphthenate;, silver naphthenate, vanadium naphthenate. Alternate forms of organic metallic compounds may be substituted provided they are soluble in the oil, such as stearates, sulfonates, or porphyrins. Some examples of sulfonate forms are metal sulfonates, dodecylbenzene metal sulfonates, or metal dinonyl naphthalene disulfonate.

The prepared oil-in-aqueous phase emulsion is then fed into an ultrasonic reactor means. The reactor used to impart ultrasonic energy to a heavy hydrocarbon-in-aqueous phase emulsion will utilize conventional means for preventing ultrasound. The emulsion will be pumped continuously through the reactor chamber at a rate sufficient to yield the desired residence time which may range from 1 second to several minutes. Ultrasonic horns which generate the ultrasonic vibrations are situated through the reactor wall into the fluid. The ultrasonic horns contain piezoelectric ceramics which vibrate at a given frequency when an electrical field is applied through attached electrodes. The vibrations are conducted through the horns into the reactor by metallic rods which also amplify the sound. The acoustic frequency may range from 10 to 50 kilohertz.

The energy input by the ultrasound generators increases the bulk temperature of the reacting fluid. Therefore, the reactor will also contain cooling coils to maintain the reaction temperature at the desired level. The ultrasonic reactor operates at atmospheric pressure and at a temperature in the 50.degree. F. to 300.degree. F. range.

The reacted emulsion exiting the ultrasonic reactor will first pass to a gas/liquid separator where gaseous reaction products (H.sub.2, H.sub.2 S, CO, CO.sub.2, CH.sub.4, etc.) are separated from the bulk emulsion. Demulsifying chemicals are then added to the emulsion and it is heated to a temperature in the 150.degree. F. to 300.degree. F. range to break the oil/water emulsion. Electrostatic separators may be used to speed the oil recovery process.

The separated water (i.e., aqueous phase) from the separation process may be treated and recycled to initial aqueous phase or emulsifier composition(s) or the emulsion forming step or discharged. The recovered oil or hydrocarbon may be fractionated using conventional methods and if desired the heavier fractions may be recycled to initial hydrocarbon or to ultrasonic reactor means to the emulsion formation step for further conversion.

Thus, recapitulating by way of further explanation, in the ultrasonic reaction means, conversion of the hydrocarbon into a lighter product occurs, while reacting any contaminant native components (such as sulfur and nitrogen) within the hydrocarbon into recoverable particles. The converted mixture leaves the ultrasonic reactor means and is processed into or through separation facilities where the upgraded hydrocarbon product (i.e., a lighter hydrocarbon product having a higher API.degree. gravity or a lower molecular weight or lower viscosity) is separated from any by-products and recyclable products (e.g., unconverted hydrocarbon). The recyclable product can be recycled back to the ultrasonic reactor means and/or to the formation (i.e., agitation) step for admixing with incoming or initial hydrocarbon being employed to form oil-in-aqueous phase emulsion.

In a preferred embodiment of the present invention, any of the emulsifying agent(s) and/or emulsifying composition(s) of this invention may be employed as fluid or processing material or injection fluid in the method of in situ bitumen recovery by percolation fully described in U.S. Pat. No. 4,406,499 (Sep. 27, 1983) to Erdal Yildirim. This United States patent is fully incorporated herein by reference thereto as if the entire wording and disclosure (including drawings) followed hereafter verbatim.

It has been further discovered that if a mixture of the hydrocarbon and the emulsifying composition(s) is agitated (i.e. by dynamic mixer agitation and/or static mixer agitation, not necessarily in the order noted) after heating the mixture to a temperature above 200.degree. F. (preferably above 200.degree. F. to about 600.degree. F., more preferably 200' F. to 280.degree. F., and under pressure as stated below), an oil-in-aqueous phase emulsion is formed having a greater or enhanced stability when compared to an oil-in-aqueous phase emulsion formed where the mixture of the hydrocarbon and the emulsifying composition(s) was not heated to a temperature above 200.degree. F. As previously indicated, a temperature above 200.degree. F. is the phase inversion temperature for a typical oil-in-aqueous phase emulsion containing a typical hydrocarbon (e.g. crude oil) wherein an oil-in-aqueous phase emulsion inverts into an aqueous phase-in-oil emulsion possessing an oil continuous phase. Thus, in another embodiment of the present invention, the hydrocarbon and the emulsifying composition(s) are initially separately heated and then admixed into a mixture having a temperature above 200.degree. F. (preferably from above 200.degree. F. to about 600.degree. F., and under pressure as stated below); and subsequently agitated (i.e. in a dynamic mixer and/or in a static mixer) to form an oil-in-aqueous phase emulsion that possesses a greater or enhanced stability than if the oil-in-aqueous phase emulsion is formed when the mixture of hydrocarbon and emulsifying composition(s) is at a temperature below 200.degree. F. Alternatively, the hydrocarbon and the emulsifying composition(s) may be initially mixed together into a mixture, and the mixture then heated to a temperature above 200.degree. F., and subsequently agitated to form an oil-in-aqueous phase emulsion. Preferably, the hydrocarbon and the emulsifying composition(s) are initially individually, separately heated to any separate respective temperatures possessing a value such that when the hydrocarbon and the emulsifying composition(s) are admixed into a mixture, the mixture possesses a temperature value above 200.degree. F. The separate, respective temperatures for the hydrocarbon and the emulsifying composition(s) to effect an above 200.degree. F. mixture would obviously depend on the quantity of both the hydrocarbon and the emulsifying composition(s) that are to be admixed.

The emulsifying composition(s) employed for the embodiment of the invention is any of above mentioned emulsifying composition(s) of this invention which will form an oil-in-aqueous phase emulsion when mixed with a hydrocarbon, and subsequently agitated (i.e. statically and/or dynamically) when the mixture of the hydrocarbon and the emulsifying composition(s) is at a temperature above 200.degree. F. Preferably, the emulsifying composition(s) are those emulsifying composition(s) containing those emulsifying agents(s) selected from the ethoxylated alkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 1966 to about 9188, and the general formula(5) above wherein in general formula (5) above n.sub.1 is an integer and has a value of from about 7 to about 20, preferably 11, and y.sub.1 is an integer having a value of from about 4 to about 1000; and wherein at least about 50% by weight of the emulsifying agents(s) comprises the ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188. The emulsifying agents(s) has at least one ethoxylated alkylphenol compound having the general formula(5A) above wherein in general formula (5A) above n.sub.1 has a value of from about 7 to about 20, preferably 11; and y.sub.1 is greater than 100, preferably greater than 100 but less than 1000, and the ethoxylated alkylphenol compound of general formula (5A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s). Preferably further, the emulsifying composition(s) are those emulsifying composition(s) containing those emulsifying agent(s) selected from the ethoxylated dialkylphenol compounds having a molecular weight distribution with a dispersity of from about 1.0 to about 5.0, a weight average molecular weight of from about 2519 to about 11,627, and the general formula (6) above wherein in general formula (6) above n.sub.1 is an integer and has a value of from about 7 to about 18, n.sub.2 is an integer and has a value of from about 7 to about 18, and y.sub.2 is an integer having a value of from about 4 to about 1000; and wherein at least about 50% by weight of the emulsifying agent(s) comprises the ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627. The emulsifying agent(s) has at least one ethoxylated dialkylphenol compound having the general formula (6A) above wherein in general formula (6A) above wherein n.sub.1 has a value of from 7 to about 18, n.sub.2 has a value of from about 7 to about 18, and y.sub.2 is greater than 100, preferably greater than 100 but less than 1000; and the ethoxylated dialkylphenol compound of general formula (6A) preferably comprises at least 1% by weight (more preferably from 1% to 90% by weight) of the emulsifying agent(s).

As previously indicated for the embodiments of the present invention, the emulsifying agent(s) contained in the emulsifying composition(s) which will be mixed with a hydrocarbon and heated to above 200.degree. F. before agitation may be a combination of the ethoxylated alkylphenol compounds having the general formula (5) and the ethoxylated dialkylphenol compounds having the general formula (6)] in any percent by weight proportion provided that the dispersity of the molecular weight distribution of the entire combination is from about 1.0 to about 5.0 (more preferably about 1.0 to about 2.5 and most preferably about 1.0 to 2.0), and the weight average molecular weight in the combination of the emulsifying agent(s) [or in general formula (5) and/or in general formula (6) is about 1966 to about 11,627 (more preferably about 3726 to about 8547, most preferably about 4606 to about 7227). Furthermore, the entire combination should comprise at least 50% by weight (more preferably at least about 70% by weight, most preferably at least 85% by weight) of the ethoxylated alkylphenol compound and the ethoxylated dialkylphenol compound wherein the ethoxylated alkylphenol compound has a molecular weight of from about 1966 to about 9188 and the ethoxylated dialkylphenol compound ha a molecular Weight of from about 2519 to about 11,627. More preferably, as previously indicated, the compounds having the general formula (5) are from about 30% by weight to about 80% by weight of the combination. Furthermore, as further previously indicated, at least 1% by weight (preferably 1% to 90% by weight) of the combination of the ethoxylated alkylphenol compound having the general formula (5) and the ethoxylated dialkylphenol compound having the general formula (6) comprises the ethoxylated alkylphenol compound having the general formula (5A) and/or the ethoxylated dialkylphenol compound having the general formula (6A), where y.sub.1 and y.sub.2 are both greater than 100, preferably greater than 100 but less than 1000.

The amount of emulsifying agent(s) used in this embodiment of the present invention, particularly when the preferred emulsifying agent(s) represented by general formula(s) (5) and/or (6) are employed, may range from about 25 (or less) to about 15,000 (or more) ppm weight-to-weight of the hydrocarbon, preferably from about 300 to about 5,000 ppm by weight. Stated alternatively, the emulsifying composition(s) of this preferred embodiment of the present invention, preferably comprises from about 0.05 vol. % to about 4.0 vol. % of the emulsifying agent(s), particularly when the preferred emulsifying agent(s) represented by general formula(s) (5) and/or (6) are used.

The hydrocarbon employed for this embodiment of the invention is any hydrocarbon which will form an oil-in-aqueous phase emulsion when mixed with the emulsifying composition(s) of the present invention (preferably those emulsifying composition(s) containing the emulsifying agents represented by the general formula(s) (5) and/or (6)); and subsequently agitated (i.e. statically and/or dynamically) when the mixture of the hydrocarbon and the emulsifying composition(s) is at a temperature above 200.degree. F., preferably above 205.degree. F. Preferably, the hydrocarbon is any hydrocarbon produced from the distillation of crude oil (i.e. crude oil produced from a well bore) into fractions according to boiling point as fully described in "Petroleum Refining" by James H. Gary and Glenn E. Handwerk (copyrighted 1975 by publisher Marcel Dekker Inc., 270 Madison Avenue, N.Y., N.Y. 10016), and in "Petroleum Refinery Engineering" by W. L. Nelson (copyrighted 1958 and copyright renewed 1969 by publisher McGraw-Hill Inc., New York, N.Y.), and in "The Chemistry and Technology of Petroleum" by James G. Speight (copyrighted in 1980 by Marcel Dekker Inc.). All of these publications are fully incorporated herein by reference thereto. Preferably, the hydrocarbon for this preferred embodiment of the present invention is a hydrocarbon produced from distillation of crude oil and has a TBP (true boiling point) at a temperature of about 650.degree. F. and higher, say 975.degree. F. and above such as up to about 1100.degree. F. and higher. Hydrocarbons having a nominal TBP at a temperature of about 650.degree. F. and above have been termed "atmospheric residiums", or long resids. Hydrocarbons having a nominal TBP cut point at a temperature of about 975.degree. F. and higher have been termed short residua, vacuum residua, pitch, asphalt etc. More preferably for this embodiment of the present invention, especially when the emulsifying agents represented by the general formula(s) (5) and/or (6) are contained in the emulsifying composition(s), the hydrocarbon is selected from the group consisting of atmospheric residiums or residua (with a TBP of between about 650.degree. F. to about 750.degree. F.) and vacuum residiums or residua (with a TBP of between about 950.degree. F. to about 1100.degree. F. and higher), and mixtures thereof.

Separation of crude oil by distillation into fractions according to boiling point to produce the hydrocarbon employed in a preferred embodiment of the present invention is typically performed or accomplished in the following two steps as set forth in the publications listed in the immediate foregoing paragraph: first, by fractionating the total crude oil in an atmospheric still/tower/fractionator at essentially atmospheric pressure to produce high-boiling bottoms fraction (termed "reduced crude" or "topped crude" or "atmospheric residiums" or "atmospheric bottoms"); and then feeding the high-boiling bottom fraction from the atmospheric still/tower/fractionator to a second still/tower/fractionator operated as a high vacuum fractionator. As is well known to those skilled in the art, the atmospheric still/tower/fractionator is initially used to produce various hydrocarbon fractions (e.g. butanes and lighter; LSR(light straight-run gasoline); naphtha; kerosine; LGO (light gas oil); and atmospheric gas oil) whose TBP (true boiling point) temperatures are below about 650.degree. F. The vacuum still/tower/fractionator is employed subsequent to the atmospheric still/tower/fractionator to separate the heavier portions from the crude oil into fractions because the high temperatures (i.e. above about 650.degree. F.) that are necessary to vaporize the high-boiling bottoms fraction at atmospheric pressure cause thermal cracking to occur, with the results being hydrocarbon loss to dry gas, discoloration of the product, and equipment fouling due to coke formation. Stated alternatively as is further well known, vigorous decomposition of crude fractions/cuts/stocks starts to take place at temperatures exceeding about 650.degree. F., and for this reason many fractions/cuts/stocks (e.g. reduced or topped crude oil, tars, vacuum gas oil (VGO), heavy gas oil (HGO), etc) cannot be distilled at atmospheric pressure. Thus, the vacuum still/tower/fractionator is needed to distill these fractions/stocks/cuts which have such high boiling ranges.

The following Table A taken from the publication above entitled "Petroleum Refining" to Gary et al contains a list of boiling ranges of typical crude oil fractions:

TBP cut points for various crude oil fractions are given in the following Table B which was also taken from the publication above entitled "Petroleum Refining" to Gary et al:

As previously indicated, in a preferred embodiment of the present invention, the hydrocarbon employed to be mixed with the emulsifying composition(s) (especially those emulsifying composition(s) containing the emulsifying agents represented by the general formula(s) (5) and/or (6)) to form a mixture, which mixture is then heated to temperature above 200.degree. F. and subsequently agitated to form an oil-in-aqueous phase emulsion, is preferably selected from the group consisting of atmospheric residiums or residua (or atmospheric bottoms) with a TBP of above about 650.degree. F., light vac gas oil (or light gas oil) with a TBP of between about 650.degree. F. to about 800.degree. F., heavy vac gas oil (or heavy gas oil) with a TBP of between about 800.degree. F. to about 950.degree. F., and asphalt (or vacuum reduced crude or vacuum gas oil or vacuum residiums or residua/bottoms) with a TBP of above about 950.degree. F. and mixtures thereof. More preferably, the hydrocarbon is selected from the group consisting of atmospheric residiums or residua and vacuum residiums or residua, and mixtures thereof. It should be understood that the hydrocarbon with a TBP above about 650.degree. F. and employed in this invention does not have to have its genesis from a virgin crude, but may be a product resulting from upgrading heavy bottoms by any suitable hydrogenation process such that the resulting hydrogenated product is a hydrocarbon with a TBP above about 650.degree. F. Heavy bottoms which may be hydrogenated typically originate from the bottom of a deasphalter and the like.

Agitation (i.e. static mixer agitation and/or dynamic mixer agitation) of the mixture of the hydrocarbon and the emulsifying composition(s) after heating the mixture to a temperature above 200.degree. F. (preferably from about 205.degree. F. to about 220.degree. F.) is preferably performed under pressurized conditions. In a preferred embodiment of the present invention, the pressure of the heated mixture is from about 25 p.s.i. to about 1,500 p.s.i.; more preferably from about 75 p.s.i. to about 625 p.s.i.; and most preferably from about 200 p.s.i. to about 410 p.s.i. When the heated mixture of the hydrocarbon and the emulsifying composition(s) is agitated with a static mixer, a pressure differential across the static mixer is needed to cause the heated mixture to flow through the static mixer. The static mixer pressure differential is preferably from about 100 p.s.i. to about 500 p.s.i.; more preferably from about 150 p.s.i. to about 325 p.s.i.; most preferably from about 180 p.s.i. to about 260 p.s.i. Because a static mixer pressure differential is necessary when the heated mixture is to be agitated with a static mixer, inlet pressurized conditions for the heated mixer at the inlet of the static mixer is preferably from about 125 p.s.i. to about 1,500 p.s.i.; more preferably from about 175 p.s.i. to about 625 p.s.i.; most preferably from about 200 p.s.i. to about 410 p.s.i.

Agitation of the mixture of the hydrocarbon and the emulsifying composition(s) after heating the mixture to a temperature above 200.degree. F. may be performed in accordance with any of the previously mentioned suitable procedures including the producing of a multimodal oil-in-aqueous phase emulsion. More specifically, agitating may comprise positioning a portion of the heated mixture in a first agitator (i.e. a first shearing and mixing means) having a predetermined shear rate to produce an oil-in-aqueous phase emulsion with a viscosity that is known or could be determined, leaving a remaining portion of the heated mixture that is not positioned in the first agitator. The remaining portion of the heated mixture is positioned in a second agitator (i.e. a second shearing and mixing means) having a predetermined shear rate that is different and not equal to the predetermined shear rate of the first agitator. The second agitator also produces an oil-in-aqueous phase emulsion with a viscosity that is known or could be determined. When the oil-in-aqueous phase emulsion from the first agitator is mixed with the oil-in-aqueous phase emulsion from the second agitator, a multimodal oil-in-aqueous phase emulsion is formed that has a lower viscosity than the viscosity of the oil-in-aqueous phase emulsion produced from the first agitator and/or lower than the viscosity of the oil-in-aqueous phase emulsion produced from the second agitator.

The first agitator and the second agitator may be arranged in any suitable position with respect to each other; and the first agitator and the second agitator may be a static shearing and mixing device and/or a dynamic shearer and mixer, and/or any other suitable means for agitating to form an oil-in-aqueous phase emulsion. In this embodiment of the present invention as was seen for other previously mentioned embodiments of the invention, a bimodal or multimodal oil-in-aqueous phase emulsion(s) may be formed with two or more static shearing and mixing device(s) in parallel, with two or more dynamic shearers and mixers in parallel, or with one (or more) dynamic shearers and mixers in parallel with one (or more) static shearing and mixing device, such as device 108. A multimodal oil-in-aqueous phase emulsion(s) may also be formed with the heated mixture by varying the residence times and/or shear rate of the heated mixture in any suitable dynamic shearer and mixer, and collecting the effluent oil-in-aqueous phase emulsion(s) leaving the dynamic shearer and mixer at various residence times and/or shear rates in any suitable tank or container. A multimodal oil-in-aqueous phase emulsion(s) may be further also formed by varying the flow rate (and the shear rate) of the heated mixture through a single static shearing and mixing device (e.g. device 108), and collecting the effluent oil-in-aqueous phase emulsion(s) produced from the single static shearing and mixing device at various flow (and shear) rates in a suitable container such as the emulsion tank 122. Regardless how the effluent oil-in-aqueous phase emulsion(s) is formulated, the produced oil-in-aqueous phase emulsion(s) has a lowered viscosity.

More specifically, the collected effluent oil-in-aqueous phase emulsion(s) produced from various flow rates of the heated mixture through a single static shearing and mixing device mixes and combines in a container to form bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity than the viscosity of oil-in-aqueous phase emulsion(s) produced from the single static shearing and mixing device with one flow (and shear) rate. Thus, by way of example only, the viscosity of a bimodal oil-in-aqueous phase emulsion(s) produced by flowing the heated mixture through a single static shearing and mixing device (such as device 108) at 40 in./sec., and combining the resulting oil-in-aqueous phase emulsion(s) with the oil-in-aqueous phase emulsion(s) formulated from subsequently flowing the same heated mixture through the same single static shearing and mixing device at 20 in./sec., would be lower than the respective viscosities of the oil-in-aqueous phase emulsion(s) produced in the single static shearing and mixing device at 40 in./sec. or 20 in./sec. Similarly, the collected effluent oil-in-aqueous phase emulsion(s) produced from agitating the heated mixture in any suitable dynamic shearer and mixer at various residence times and/or shear rates combine and mix in a tank or container to form a bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity than oil-in-aqueous phase emulsion(s) produced from one dynamic shearer and mixer having an affixed (or constant) shear rate and/or residence time of the heated mixture in the same dynamic shearer and mixer. For example and by way of example only, the viscosity of a bimodal oil-in-aqueous phase emulsion(s) produced by positioning for 4 secs. the heated mixture in a dynamic shearer and mixer having a shear field intensity of 500 sec..sup.-1, and combining the resulting oil-in-aqueous phase emulsion(s) with the oil-in-aqueous phase emulsion(s) formulated from subsequently positioning for 4 secs. the same heated mixture in the same dynamic shearer and mixer having a shear field intensity of 6,000 sec..sup.-1, would be lower than the respective viscosities of the oil-in-aqueous phase emulsion(s) produced with an intensity of 500 sec..sup.-1 or 6,000 sec..sup.-1. Similar results can be obtained by varying the residence time while holding the shear field intensity generally constant or fixed.

More specifically further, the collected effluent oil-in-aqueous phase emulsions produced from two (or more) dynamic shearers and mixers having different shear rates (or shear field intensities) and/or with different residence times for the heated mixture of emulsifying composition(s) and crude in the respective dynamic shearers and mixers combine to form bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lower viscosity than the viscosity of oil-in-aqueous phase emulsion(s) produced from any one of two (or more) dynamic shearers and mixers having the same shear rate (or shear field intensity) and/or same residence time for the heated mixture. Similarly, the collected effluent oil-in-aqueous phase emulsions produced from one (or more) dynamic shearers and mixers and/or one (or more) static shearing and mixing devices in parallel with one (or more) static shearing and mixing devices and/or one (or more) dynamic shearers and mixers combine to form bimodal or multimodal oil-in-aqueous emulsion(s) having a lower viscosity than the viscosity of oil-in-aqueous phase emulsion(s) produced from any single one dynamic shearer and mixer or from any single one static shearing and mixing device. Typically, each dynamic shearer and mixer has a different shear rate (or shear field intensity), and/or the residence times for the heated mixture in each dynamic shearer and mixer are distinct from each other.

Typically further, each static shearing and mixing device has or produces a different shear rate from the other static shearing and mixing devices. Thus, by way of example only, a bimodal or multimodal oil-in-aqueous phase emulsion may be produced by positioning for a generally known period (e.g. 0.10 sec. to 5 mins. or higher) a portion of the heated mixture (i.e. heated to a temperature above 200.degree. F.) in a first dynamic shearer and mixer having a predetermined or known shear rate (e.g. a shear field intensity from 50 sec..sup.-1 to about 10,000 sec..sup.-1 or higher) to produce a first oil-in-aqueous phase emulsion having a first viscosity, leaving a remaining portion of the heated mixture that has not been positioned in the first dynamic shearer and mixer. The remaining heated mixture is positioned for a generally known period of time in a second dynamic shearer and mixer (or passed through a static shearing and static mixing device at a predetermined velocity for a predetermined period of time). The second dynamic shearer and mixer has a shear rate that is different from the shear rate of the first dynamic shearer and mixer, and produces a second oil-in-aqueous phase emulsion having a second viscosity. When the first oil-in-aqueous phase emulsion is mixed or commingled with the second oil-in-aqueous phase emulsion, an oil-in-aqueous phase emulsion is produced having a viscosity lower than the first viscosity of the first oil-in-aqueous phase emulsion and lower than the second viscosity of the second oil-in-aqueous phase emulsion. The one or more dynamic shearers and mixers and/or one or more static shearing and mixing devices may be in any relationship to each other, such as in parallel or in series. Thus, one (or more) dynamic shearing and mixing devices may be disposed in parallel with one (or more) dynamic shearing and mixing devices and/or one (or more) static shearing and mixing devices; or one (or more) static shearing and mixing devices may be disposed in parallel with one (or more) static shearing and mixing devices; or one (or more) static shearing and mixing devices or one (or more) dynamic shearing and mixing devices may be disposed in series with one (or more) static shearing and mixing devices or one (or more) dynamic shearing and mixing devices; all (of the immediate foregoing) for producing a bimodal or multimodal oil-in-aqueous phase emulsion(s) having a lowered viscosity.

In a preferred embodiment of the present invention, the heated mixture (i.e. heated to a temperature above 200.degree. F.) of hydrocarbon and the emulsifying composition(s) is agitated in a static shearing and mixing device having 12 or more mixing elements; identified as baffle element 156 in FIG. 5 or baffle element 158 in FIG. 6 or baffle element 180 in FIG. 11 or baffle element 208A or 208B in FIG. 14. Preferably, the static shearing and mixing device (i.e. device 108) has from 16 to 31 baffle elements, more preferably 32 or more baffle elements are used. As previously indicated, that static mixer pressure differential is from about 100 p.s.i. to about 500 p.s.i.; more preferably from about 150 p.s.i. to about 325 p.s.i.; most preferably from about 180 p.s.i. to about 260 p.s.i. It has been discovered that a static shearing and mixing device with 32 baffle elements and with a static mixer pressure differential of from about 180 p.s.i. to about 260 p.s.i. produces an oil-in-aqueous phase emulsion with improved stability (i.e. improved shear life) when compared with an oil-in-aqueous phase emulsion produced in a static shearing and mixing device having 16 baffle elements and with the same static mixer pressure differential of from about 180 p.s.i. to about 260 p.s.i., especially when the hydrocarbon has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (e.g. atmospheric residua), more preferably when the hydrocarbon has a nominal TBP cut point exceeding a temperature of about 950.degree. F. and above (e.g. a vacuum residua).

As has also been previously indicated, the oil droplet size within an oil-in-aqueous phase emulsion may be predicted by the following equations:

where d is the volumetric mean oil droplet size in microns; C is a constant ranging from about 750 to about 1,500 and represents a multiplier contributing to the absolute disposition in volumetric mean droplet size of the oil; D is the internal diameter in inches for the static shearing and mixing device (i.e. device 108); N.sub.we is the dimensionless Weber Number for the fluid flowing through the static shearing and mixing device and ranges from about 50 to about 30(10.sup.6); a is an exponent which is from about 0.3 to about 1.2, preferably about 0.6; and b is also an exponent ranging in value from about 0.2 to about 0.8, preferably about 0.4. The exponents a and b are constants, which account for the relative variation in the volumetric means droplet size of the oil. As was previously mentioned, N.sub.we is the Weber Number, a commonly used dimensionless number relating shear forces imparted on the oil droplet to the cohesive forces holding the oil drop together, defined as ##EQU6## where D is the internal diameter in inches of the static shearing and mixing device; v is the velocity in inches per second of the fluid flowing through the static shearing and mixing device; .rho. is the oil-in-aqueous phase emulsion density in lbs. per cubic foot; and .delta. is the interfacial tension for the oil-in-aqueous phase emulsion in dynes per cubic centimeter. As stated above, the oil-in-aqueous phase emulsion density .rho. ranges from about 40 lbs./ft.sup.3 to about 70 lbs/ft.sup.3 ; and the interfacial tension .delta. for the oil-in-aqueous phase emulsion ranges from about 0.25 dynes/cm..sup.3 to about 25 dynes/cm.sup.3.

The oil-in-aqueous phase emulsion produced from one (or more) static shearing and mixing devices may typically contain oil droplets having a particle size larger than 100 microns. In a preferred embodiment of the present invention, especially when the oil droplets in an oil-in-aqueous phase emulsion are from a hydrocarbon having a nominal TBP at a temperature of about 650.degree. F. and above (more preferably about 950.degree. F. and above) and the oil-in-aqueous phase emulsion is produced for burning purposes, the produced oil-in-aqueous phase emulsion is subsequently passed through a homogenizing device for lowering the particle size of those oil droplets having a particle size greater than 100 microns (such as 200 or 250 microns or higher) to a particle size 100 microns or below. The 100 micron and larger particles may result from coalscence during handling and/or storage as well as the manufacturing method. The homogenizing device may be any suitable device or means (e.g. a dynamic shearing and mixing means) for lowering oil droplet sizes greater than 100 microns to below 100 microns. A suitable homogenizing device employed in the laboratory has been found to be a Gaulin Model 15 M-8TA laboratory homogenizer, manufactured by Gaulin Corporation, Garden Street, Everett, Mass. 02149.

After the heated mixture (i.e. heated above 200.degree. F.) of the hydrocarbon and the emulsifying composition(s) has been agitated in accordance with any of the previously mentioned procedures to formulate an oil-in-aqueous phase emulsion, the formulated oil-in-aqueous phase emulsion is subsequently cooled to below 200.degree. F. (preferably below about 175.degree. F., more preferably below about 150.degree. F., most preferably below about 120.degree. F.) and may be transported, such as in a vessel or through a pipeline (or the like) for any suitable purposes, such as for burning in a boiler (or the like) to produce heat, power and the like. Cooling of the formulated oil-in-aqueous phase emulsion is preferably accomplished as soon as possible after formulation, such as from within one (1) sec. to about five (5) minutes, more preferably from about one (1) sec. to about three (3) minutes. Before cooling, the formulated oil-in-aqueous phase emulsion contains oil droplets, essentially or substantially all of which should have a particle size of 100 microns or below. Preferably, no more than about 5% by wt. of the oil in any given volume of formulated oil-in-aqueous phase emulsion has a particle size larger than 100 microns (especially larger than between 100 microns and 250 microns or above 250 microns); more preferably, no more than 3% by wt. of the oil in any given of volume of the formulated oil-in-aqueous phase emulsion has a particle size larger than 100 microns (especially larger than between 100 microns and 250 microns or above 250 microns); and most preferably, 1% by wt. or less of the oil in any given volume of the formulated oil-in-aqueous phase emulsion has a particle size 100 microns and/or less than 100 microns. Ideally, there are essentially no oil droplets in any given volume of formulated oil-in-aqueous phase emulsion which have a droplet size above 100 microns, especially when the formulated oil-in-aqueous phase emulsion is to be burned and the hydrocarbon (or oil droplets) has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (more preferably of about 950.degree. F. and above). As have been previously indicated, as long as the temperature of oil-in-aqueous phase emulsion(s) is below about 120.degree. F., there should be no problems with the oil-in-aqueous phase emulsion(s) with respect to stability. Similarly, as long as the quantity of aqueous phase in the formulated oil-in-aqueous phase emulsion(s) is greater than what is needed, there should be no problems with the oil-in-aqueous phase emulsion(s) with respect to pipeline-viscosity standpoint, especially for when the hydrocarbon has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (more preferably of about 950.degree. F. and above). Excess aqueous phase in the oil-in-aqueous phase emulsion(s) is of no major concern when the oil-in-aqueous phase emulsion(s) is to be transported through a pipeline that is not too long, such as one (1) to two (2) miles. However, excess aqueous phase for combustion may be limited. Once the amount aqueous phase in the formulated oil-in-aqueous phase emulsion(s) is the appropriate amount for an effective pipeline-viscosity, the formulated oil-in-aqueous phase emulsion(s) may be pumped or transported through a pipeline of any length without any fears or concerns about the formulated oil-in-aqueous phase emulsion(s) failing and/or breaking down into a mixture of phases that do not possess an effective viscosity for pipeline transportation and/or for burning purposes. As was previously mentioned, one of the salient features of the oil-in-aqueous phase emulsion(s) of this invention is that although the formulated oil-in-aqueous phase emulsion may fail and/or break down in a container or pipeline into a mixture comprising an at least partially (i.e. partially or substantially) coalesced oil droplets in the aqueous phase emulsion(s), the mixture has a viscosity that is less than or equal to the viscosity of the original oil-in-aqueous emulsion(s) in spite of the fact that the coalesced oil droplet phase itself has a viscosity larger than the viscosity of the original oil-in-aqueous emulsion(s). It should be understood that the mixture may include some (but not a substantial amount of) formed oil-in-aqueous phase emulsion that has inverted into an aqueous phase-in-oil emulsion. Such aqueous phase-in-oil emulsion may be part of the coalesced oil droplet phase and/or the residual oil-in-aqueous phase emulsion and/or separate from both the coalesced oil droplet phase and the residual oil-in-aqueous phase emulsion. With the emulsifier agent(s) of this invention (i.e. those emulsifier agent(s) represented by general formula(s) (5) and/or (6)) in combination with other features of this invention, when the oil-in-aqueous emulsion(s) fail or breakdown in a container or a pipeline into the mixture comprising at least partially coalesced oil droplets and a residual oil-in-aqueous phase emulsion(s), a substantial proportion of the original, formulated oil-in-aqueous emulsion(s) is not inverted into a aqueous phase-in-oil emulsion. As previously mentioned for earlier embodiments of the present invention, the residual oil-in-aqueous phase emulsion(s) may be defined as the remaining oil-in-aqueous phase emulsion(s) from the original oil-in-aqueous phase emulsion(s) whose contained dispersed oil droplets have not at least partially coalesced. These features of the present invention enable the mixture comprising the at least partially coalesced oil droplets and residual oil-in-aqueous phase emulsion to be continuously pumped or otherwise transported through the same pipeline that the original oil-in-aqueous phase emulsion(s) was introduced into, without the need for removing the mixture to reformulate the oil-in-aqueous phase emulsion(s). However, one of the desirable qualities of the oil-in-aqueous phase emulsion(s) of this invention is that if there is a breakdown or failure in the original oil-in-aqueous phase emulsion(s) into the coalesced oil droplet-residual emulsion mixture, the original oil-in-aqueous phase emulsion(s) may be easily reformulated by merely passing the mixture through another device (e.g. a static mixer and/or a dynamic mixer, a homogenizer, a pump, etc.) which may be situated within the vessel or the pipeline that is transporting the oil-in-aqueous phase emulsion(s). Thus, if desired, such reformulation may be easily accomplished even though it is not necessary to do so to continue the pumping or transportation of the failed or broken down original oil-in-aqueous phase emulsion(s).

The emulsifying agent(s) of this invention (i.e. those represented by general formula(s) (5) and/or (6)) used in the preparation of the oil-in-aqueous phase emulsions at a temperature above 200.degree. F. may gradually become inactivated during pipeline flow (or other means of transportation) after cooling depending on the original concentration or quantity of emulsifying agent(s) employed, the temperature of the emulsion-forming constituents (i.e. crude or hydrocarbon and emulsifying composition) at formulation, etc. Regardless of any formulation condition, the formed oil-in-aqueous phase emulsion will eventually separate into the two-phase mixture (i.e. the coalesced oil droplet-residual emulsion mixture) which, as was indicated above, will continue to flow under ordinary circumstances. The total distance through a pipeline in which an oil-in-aqueous phase emulsion may be pumped or otherwise transported prior to separation into the two-phase mixture also depends on the original concentration or quantity of the emulsifying agent(s) employed, and the temperature of the emulsion forming constituents at formulation, as well as other properties of the hydrocarbon crude oil and aqueous phase and container or pipeline and pumping conditions. If, for any reason, the oil-in-aqueous phase emulsion can not be prepared with sufficient stability to be pumped (or otherwise transported) over the total length of a pipeline, another embodiment of the present invention provides for remedial procedures to restore the oil-in-aqueous emulsion in order to allow for the continued transportation of the formed oil-in-aqueous emulsion through a pipeline for any desired distance. More specifically, it has been discovered that through the addition of additional aqueous phase and/or the addition of additional concentrated emulsifying composition [or additional pure emulsifying agent(s)] into the vessel or pipeline that has been transporting the original formed oil-in-aqueous phase emulsion that has separated into the two-phase mixture (or the coalesced oil-droplet-residual emulsion mixture), the separated oil-in-aqueous phase emulsion can be restored into the original formed oil-in-aqueous phase emulsion with sufficient agitation, such as by pumping or mixing or shearing or the like. The selection of additional aqueous phase and/or additional concentrated emulsifying composition [or pure emulsifying agent(s)] depends on the condition or state of the separated oil-in-aqueous phase emulsion, the pipeline and pumping conditions, the desires of the pipeline operator and refiner or other receiver of the oil-in-aqueous phase emulsion, and etc. Depending further on the pipeline and pumping conditions, it has been discovered that should even the original formed oil-in-aqueous emulsion completely fail or otherwise transform into a highly viscous oil continuous system, such oil continuous system can be restored into the original formed oil-in-aqueous phase emulsion through the addition or injection in to the pipeline of additional emulsifying composition along with agitation, such as pumping or shearing and mixing statically. The use of this technique to correct a total oil-in-aqueous phase emulsion failure would require that the necessary quantities of emulsifying composition be available and injection pumps be located at the location in the pipeline where the total failure has occurred.

In another preferred embodiment of the invention, the prepared oil-in-aqueous phase emulsion is a double emulsion. The hydrocarbon may be any hydrocarbon as previously defined, but is preferably the hydrocarbon that has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (more preferably about 950.degree. F. and above). The double emulsion for this embodiment of the invention is formed by dispersing through agitation (i.e. statically shearing and mixing and/or dynamically shearing and mixing) an aqueous phase in a hydrocarbon containing an emulsifying agent(s) to form an aqueous phase-in-oil emulsion [i.e. an oil continuous emulsion (OCE)]; and subsequently agitating (i.e. statically shearing and mixing and/or dynamically shearing and mixing) the initially formed aqueous phase-in-oil emulsion with the emulsifying composition containing the emulsifying agent(s) represented by general formula(s) (5) and/or (6) to form the double emulsion oil-in-aqueous phase emulsion. The emulsifying agent(s) that are contained in the hydrocarbon and/or aqueous phase to form the OCE may be any emulsifying agent capable of forming the OCE but is preferably those nonionic emulsifying agent(s) having the general formula: ##STR34## where n is from about 7 to about 20, preferably 7 to 9, and y is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 2 to about 15, preferably from about 7 to about 11, more preferably about 9; and/or ##STR35## wherein n.sub.1 is from about 7 to about 18, preferably about 8, n.sub.2 is from about 7 to about 18, preferably about 8, and y.sub.1 is an integer that represents the average number of ethylene oxide units or segments in the emulsifying agent(s), which is the mean of a normal Gaussian distribution curve and is from about 2 to about 15, preferably from about 7 to about 11, more preferably about 9. If a combination of the compounds having the general formula (9) and the compounds having general formula (10) are employed, the compounds having the general formula (10) are preferably at least 40% by weight of the combination. More preferably, the compounds having general formula (10) are from about 50% by wt. to about 85% by wt. of the combination.

If the hydrocarbon for the double emulsion has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (more preferably about 950.degree. F. and above), the double emulsion for this embodiment of the invention is formed by initially dispersing by agitating (i.e. statically shearing and mixing and/or dynamically shearing and mixing) at a temperature above 200.degree. F. (i.e. a temperature preferably from above 200.degree. F. to about 280.degree. F.) and under pressure (i.e. a pressure of from about 100 p.s.i. to about 500 p.s.i.) an aqueous phase in the hydrocarbon, preferably containing the emulsifying agent(s) having general formula(s) (9) and/or (10), to form an aqueous phase-in-oil emulsion [i.e. an oil continuous emulsion (OCE)]; and subsequently agitating (i.e. statically shearing and mixing and/or dynamically shearing and mixing) under pressure (i.e. a pressure of from about 100 p.s.i. to about 500 p.s.i.) at a temperature above 200.degree. F. (i.e. a temperature preferably from above 200.degree. F. to about 280.degree. F.) the initially formed aqueous phase-in-oil emulsion with the emulsifying composition containing the emulsifying agent(s) represented by general formula(s) (5) and/or (6).

In a preferred embodiment of the present invention, dispersing the aqueous phase into the hydrocarbon is preferably accomplished by initially admixing the aqueous phase and/or the hydrocarbon with from about 100 ppm to about 1000 ppm of the emulsifying agent(s having general formula(s) (9) and/or (10) above and then agitating (or agitating simultaneously with admixing) the hydrocarbon and the aqueous phase (one or both of which contains the emulsifying agent(s) having general formula(s) (9) and/or (10)] to form an OCE containing from about 1% by wt. aqueous phase to about 10% by wt. aqueous phase (more preferably from about 6% by wt. aqueous phase to about 9% by wt. aqueous phase) and aqueous phase droplets having a mean droplet size ranging from about 1 micron to about 50 microns, more preferably ranging from about 5 microns to about 20 microns. If the hydrocarbon for the double emulsion has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (more preferably about 950.degree. F. and above), dispersing the aqueous phase into the hydrocarbon is preferably accomplished by heating the aqueous phase and/or the hydrocarbon under pressure (i.e. pressure of from about 100 p.s.i. to about 500 p.s.i.) to a temperature above 200.degree. F. (preferably from above 200.degree. F. to about 280.degree. F.) and adding to the aqueous phase and/or the hydrocarbon from about 100 ppm to about 1000 ppm of the emulsifying agent(s) having general formula(s) (9) and/or (10) above. These emulsifying agent(s) may be added to the aqueous phase and/or to the hydrocarbon. Subsequently, the heated hydrocarbon and aqueous phase (one or both of which contain the emulsifying agent(s) having general formula(s) (9) and/or (10)) are agitated (i.e. statically shearing and mixing and/or dynamically shearing and mixing) under pressure (i.e. pressure of from about 100 p.s.i. to about 500 p.s.i.) to form the aqueous phase-in-oil emulsion (or OCE).

As previously indicated, after the OCE is formulated, the OCE and the emulsifying composition containing the emulsifying agent(s) (5) and/or (6) are subsequently heated to a temperature above 200.degree. F. (if not already above 200.degree. F.) and agitated as previously indicated to formulate the double emulsion oil-in-aqueous phase emulsion. This formed double emulsion oil-in-aqueous phase emulsion has a temperature above 200.degree. F. and should be subsequently cooled to below 200.degree. F. (preferably below about 175.degree. F., more preferably below about 150.degree. F., most preferably below about 120.degree. F.) Cooling of the formulated double emulsion oil-in-aqueous phase emulsion is preferably accomplished as soon as possible after formulation, such as from one (1) sec. to about five (5) minutes, more preferably from about one (1) sec. to about three (3) minutes.

In a preferred embodiment of the present invention, the formulated double emulsion oil-in-aqueous phase emulsion is for burning purposes; thus, it is important that the formulated double emulsion oil-in-aqueous phase emulsion contain an effective droplet size, both the aqueous phase droplets in the initially formed OCE and the oil droplets in the finally formulated double emulsion oil-in-aqueous phase emulsion. It has been reported that in combustion of heavy crudes, droplets larger than 260 microns in the spray contribute heavily to soot formation and that small droplets of water dispersed in the hydrocarbon can improve combustion efficiency by vaporizing explosively in the flame. H. Whaley and G. Banks have reported (see "Combustion and Heat Characteristics of Bitumen Emulsions" presented at the International Flame Research Foundation (IFRF) 9th Members Conference, Ijmuiden, Netherlands, May, 1989) that best performance was generally observed employing from about 5% by wt. to about 20% by wt. aqueous phase dispersed in the hydrocarbon or oil. Typically, oil-in-aqueous phase emulsions contain oil droplets having a size larger than 260 microns; thus, the inclusion of small aqueous phase droplets (e.g. 1 to 50 microns) within oil droplets, especially larger oil droplets (i.e. 100 microns or larger), could effect secondary atomization and enhance combustion efficiency.

As previously indicated, it is important for combustion purposes that the aqueous phase be dispersed into the hydrocarbon with a right droplet size distribution (preferably from 1% by wt. to 10% by wt. aqueous phase in the hydrocarbon with a mean aqueous droplet size distribution ranging from 1 micron to 100 micron, preferably mostly 5 to20 microns).

The aqueous droplet size in the hydrocarbon must conform to a range such that aqueous droplets are small enough for inclusion within the oil droplets of the aqueous phase continuous emulsion, but large enough to cause explosive secondary atomization. The size of the oil droplets in the aqueous phase continuous emulsion must also be controlled to an optimum range. If the oil droplets are too large, the aqueous phase continuous emulsion lacks stability and burns poorly. If the oil droplets are too small, the aqueous phase continuous emulsion becomes excessively viscous and would require too much aqueous phase (water) to effect atomization. Preferably, the initial OCE emulsion is formed to contain from about 1% by wt. to about 10% by wt. aqueous phase with a mean aqueous droplet size ranging from about 1 micron to about 50 microns (more preferably 5 to 20 microns). Preferably further the subsequent aqueous phase continuous emulsion mixture (i.e. the double emulsion mixture) is formed with from about 20% by wt. to about 29% by wt. (more preferably from 20% by wt. to about 25% by wt.), on an absolute or total weight of the entire double emulsion mixture, aqueous phase/water with a mean oil droplet size ranging from about to 100 microns, preferably 20 to 50 microns. An homogenizer may be employed to effect the correct oil droplet size, all in accordance with the previously mentioned procedure.

Initial pilot plant tests have shown that dispersing aqueous phase into a hydrocarbon/oil with properly controlled droplet size distribution is not readily discernible to those skilled in the art. It has been discovered that acceptable OCE was formed using a static mixer at 6% by wt. aqueous phase, but at the desired test level of 10% by wt. aqueous phase, the aqueous phase droplet size was larger (i.e. over 50 microns) than desired. Testing with dynamic mixers and a homogenizer produced similar OCE. As will be further shown in the Examples below, it has been discovered that best or optimum results in producing the initial OCE are obtained with those nonionic emulsifying agent(s) having general formula (9) above where n is about 8 and y is about 8; or stated alternatively with NP-9 (ethoxylated nonylphenol with 9 ethylene oxide repeat units).

The invention will be illustrated by the following set-forth examples which are given by way of illustration and not by any limitation. All parameters such as concentrations, mixing proportions, temperatures, pressure, rates, compounds, etc., submitted in these examples are not to be construed to unduly limit the scope of the invention.

The oil samples used for these investigations were Westmin crude. The brine was Westmin field produced with a pH of about 6.2. The surface active agents used in the testing series were ethoxylated nonyl phenols (NP). They are all members of the general family of nonionic surface active agents of the formula: ##STR36## where y=40 (NP40) and y=100 (NP 100). Various concentrations of the respective surface active agents (ranging from 214.3 ppm to about 500 ppm by weight of Westmin Crude) were mixed with the brine to form emulsifying composition(s). The emulsifying composition(s) was mixed with the Westmin crude at a temperature of 160.degree. F..+-.10.degree. F. An oil-in-water emulsion was formed with the emulsifying-crude mixture by positioning the mixture in a rotor stator mixer. Mixing energies were 3,000 rpm for 60 secs. The oil-in-water emulsion(s) produced contained from about 15 percent to about 40 percent by weight brine. The following Table I discloses shear life (which is a measure of emulsion stability) that was detected for the various concentration of emulsifiers:

A 1:1 ratio on NP40 to NP100 produced an oil-in-water emulsion with a higher shear life than the other ratios.

Repeat Example I but prepare the oil-in-water emulsion(s) only with a 2 inch diameter static shearer and mixer embodied by FIGS. 4-7 or FIGS. 8-13 or FIGS. 14-15 at a throughput velocity of from about 20 in./sec. to about 140 in./sec. and find that the shear life is greater for each ratio of NP40 to NP100 and also find that the 1:1 ratio of NP40 to NP100 produces the highest shear life when compared to the other ratios of NP40 to NP100. Thus, the oil-in-water emulsion(s) produced through a static shearer and mixer has a shear life greater than if the oil-in-water emulsion(s) was produced by dynamic mixing.

Example I was repeated for Westmin crude having a pH of about 8.5. Table II below lists the shear life that was found for various concentrations of emulsifiers:

A 1:1 ratio of NP40 to NP100 produced an emulsion with a higher shear life than the other ratios.

Repeat Example III but prepare the oil-in-water emulsion only with a 2 inch diameter static shearer and mixer embodied by FIGS. 4-7 or FIGS. 8-13 or FIGS. 14-15 at a throughput velocity of from about 20 in./sec. to about 140 in./sec. and find that the shear life is larger for each ratio of NP40 to NP100 and also find that the 1:1 ratio of NP40 to NP100 produces the highest shear life when compared to the other ratios of NP40 to NP100.

Repeat Examples I-IV but immediately cool the respective mixtures of the crudes plus the emulsifying composition below about 100.degree. F. after the formation of the emulsion and find that the shear life increases for each oil-in-water emulsion. Thus, the stability of each oil-in-water emulsion is increased by immediately cooling the formed oil-in-water emulsion below about 100.degree. F.

The oil samples used for these investigations were Jibaro crude. The brine was synthetic brine with a pH of from about 7.0.+-.1.0 and a NaCl content of from about 5.0% by wt..+-.3%. The emulsifiers used in the testing series were NP40 and NP100. Various concentrations (ranging from 0 ppm to about 1428.6 ppm by weight of Jibaro crude) of the respective surface active agents were mixed with the brine to form emulsifying composition(s). The emulsifying composition(s) was mixed with the Jibaro crude at a temperature of 160.degree. F..+-.10.degree. F. An oil-in-water emulsion was formed with emulsifier crude mixture by positioning the mixture in a rotor stator means. Mixing energies were 3,000 rpm for 40 secs. The oil-in-water emulsion(s) produced contained from about 15 percent to about 60 percent by weight brine. The following Table III disclose shear life that was detected for the various concentration of emulsifiers:

A 1:1 ratio of NP40 to NP100 produced an oil-in-water emulsion with a higher shear life than the other ratios.

Repeat Example VI but prepare the oil-in-water emulsion only with a 2 inch diameter static shearer and mixer embodied by FIGS. 4-7 or FIGS. 8-13 or FIGS. 14-15 at a throughput velocity of from about 20 in./sec. to about 140 in./sec. and find that the shear life is larger for each ratio of NP40 to NP100 and also find that the 1:1 ratio of NP40 to NP100 produces the highest shear life when compared to the other ratios of NP40 to NP100.

Repeat Examples VI-VII but immediately cool the respective mixtures of the crudes plus the emulsifier composition below about 100.degree. F. after the formation of the emulsion and find that the shear life increases for each oil-in-water emulsion. Thus, the stability of each oil-in-water emulsion is increased by immediately cooling the formed oil-in-water emulsion below about 100.degree. F.

The oil samples were Athabasca bitumen. The aqueous phase was brine comprising 3% by wt. NaCl. The emulsifier agent(s) were NP40 and NP100. A 1:1 ratio of NP40 (2857.1 ppm by weight of Athabasca bitumen) and NP100 (2857.1 ppm by weight of Athabasca bitumen) was added to the brine to form emulsifying composition(s). The emulsifying composition(s) was mixed with the Athabasca bitumen at a temperature of about 165.degree. F..+-.5.degree. F. The emulsifying-bitumen mixture was placed in a rotor-stator mixer at 3000 rpm for 40 secs. No oil-in-water emulsion(s) was produced. Thus, NP40/NP100 could not produce an oil-in-water emulsion with Athabasca bitumen.

Repeat Example IX with the emulsifying composition comprising the emulsifying agent as an ethoxylated alkyphenol compound having the general formula: ##STR37## and employed in the brine at a concentration of about 1428.6 ppm by weight of Athabasca bitumen. The emulsifying composition was mixed with the Athabasca bitumen at a temperature of about 190.degree. F..+-.5.degree. F. The emulsifying-bitumen mixture was placed in a rotor-stator at 3000 rpm for 40 secs. An oil-in-water emulsion(s) was produced. Thus, while NP40/NP100 could not produce an oil-in-water emulsion with Athabasca bitumen, the ethoxylated alkylphenol compound of this Example X does produce oil-in-water emulsion(s).

Repeat Example IX with any of the static shearer/mixer and find similar results.

Repeat Example X with any of the static shearer/mixer of this invention and find similar results.

The oil samples were Athabasca bitumen. The aqueous phase was brine comprising 3% by wt. NaCl. A 1:1 ratio of NP40 (1428.6 ppm by weight of Athabasca bitumen) and NP100 (1428.6 ppm by weight of Athabasca bitumen) was added to the brine to form an emulsifying composition(s). The emulsifying composition(s) was mixed with the Athabasca bitumen at a temperature of about 160.degree. F. The emulsifying-bitumen mixture was placed in a rotor-stator mixer at 3000 rpm for 40 secs. An oil-in-water emulsion(s) was produced, but only with a shear life less than one(1) minute. Thus, the NP40/NP100 could not produce with Athabasca bitumen an oil-in-water emulsion with any substantial shear life.

Repeat Example XIII with the emulsifying composition comprising the emulsifying agent as an ethoxylated dialkylphenol compound having the general formula: ##STR38## and employed in the brine at a concentration of about 1428.6 ppm by weight of Athabasca bitumen. The emulsifying composition was mixed with the Athabasca bitumen at a temperature of about 190.degree. F..+-.5.degree. F. The emulsifying-bitumen mixture was placed in a rotor-stator at 3000 rpm for 40 secs. An oil-in-water emulsion(s) was produced with a substantial shear life. Thus, while NP40/NP100 could not produce an oil-in-water emulsion with Athabasca bitumen, the ethoxylated dialkylphenol compound of this Example XIV does produce oil-in-water emulsion(s).

Repeat Example XIII with any of the static shearer/mixers of this invention and find similar results.

Repeat Example XIV with any of the static shearer/mixers of the invention and find similar results.

The crude for this Example was PCEJ bitumen. The aqueous phase was brine with about 1.7% by wt. NaCl. The surfactant was a mixture of 714.3 ppm NP40 (714.3 ppm of NP40 by weight of PCEJ bitumen) and 714.3 ppm NP100 (714.3 ppm of NP100 by weight of PCEJ bitumen). The brine and surfactants were mixed to form an emulsifying composition. The emulsifying composition and PCEJ bitumen were mixed and passed at a temperature of about 180.degree. F. through a 2.07 in. diameter static mixer of FIGS. 8-13 at a rate of about 114 in./sec. to form an oil-in-water emulsion having a water concentration of about 25% by wt. The measured volumetric mean oil drop size was 27 microns. The predicted volumetric mean oil drop size from the formula d=CD.sup.a N.sub.w.sup.-b.sub.e with C=1000; a=0.5; b=0.35; D=2.07 inches; and N.sub.we =109,700, was 25 microns. Thus, the predicted volumetric mean oil drop size was comparable to the measured volumetric mean oil drop size.

The crude for this Example was Manatokan. The aqueous phase was brine with about 1.7% by wt. NaCl. The surfactant was a mixture of 714.3 ppm NP40 (714.3 ppm of NP40 by weight of Manatokan) and 714.3 ppm NP100 (714.3 ppm of NP100 by weight of Manatokan). The brine and surfactants were mixed to form an emulsifying composition. The emulsifying composition and Manatokan were mixed and passed at a temperature of about 160.degree. F. through a 0.20 in. diameter static mixer of FIGS. 4-7 at a rate of about 60 in./sec. to form an oil-in-water emulsion having a water concentration of about 28% by wt. The measured volumetric mean oil drop size was 34 microns. The predicted volumetric mean oil drop size from the formula d=CD.sup.a N.sub.w.sup.-.sub.e.sup.b with C=1000; a=0.5; b=0.35; D=0.20 inches; and N.sub.we =1,920, Was 32 microns. Thus, the predicted volumetric mean oil drop size was comparable to the measured volumetric mean oil drop size.

The Example is presented to prove that bimodal oil-in-water emulsion(s) has an improved viscosity. The crude was Manatokan. The aqueous phase was water. The surfactant was a mixture of 714.3 ppm NP40 (714.3 ppm of NP40 by weight of Manatokan) and 714.3 ppm NP100 (714.3 ppm of NP100 by weight of Manatokan). The emulsifying composition was prepared by mixing water with the surfactant. Two oil-in-water emulsions were prepared by mixing a known amount of the emulsifying composition(s) with a known amount of the Manatokan and agitating with a rotor-stator mixer having a mixer energy of 3000 rpm for 40 secs. The first oil-in-water emulsion(s) had a mean oil droplet size (.mu.) of 69.9, a dispersity of 3.27, and a viscosity (cp) of 221. The second emulsion with less Manatokan had a mean oil droplet size of 54.9, a dispersity of about 3.56, and a viscosity (cp) of about 198. When 1 liter of the first emulsion was mixed with 1 liter of the second emulsion a third oil-in-water emulsion was produced having a mean oil droplet size of about 61.7, a dispersity of about 3.88 and a viscosity (cp) of about 140. Thus, bimodal emulsion have a lower viscosity than any of its emulsion constituents.

The crude oil was Athabasca bitumen. The aqueous phase was brine comprising 3% by wt. NaCl with a pH of 7.0 to 8.0. The surfactant was a 50:50 mixture of ##STR39## The oil-in-water emulsion formation temperature was 164.degree. F. with a rotor/stator at 3000 rpm for 300 sec. The following Table IV discloses the results of six (6) experimental runs wherein biopolymer xanthan was employed in three (3) of the six (6) runs:

The above data show that a stable water continuous Syncrude bitumen emulsion formed with a dynamic rotor-stator device cannot be formed without the biopolymer xanthan acting as a continuous, water phase thickener and emulsion stabilizer, and cannot be formed below a surfactant concentration of 8,571.4 PPM.

The crude oil was Athabasca bitumen. The brine has a pH of about 8.5 and comprised 3% by wt. NaCl. The surfactant was a 50 mixture of DP150 and DNP150. The mixer Was a static mixer of FIGS. 4-7. The flow rate was between 20 in./sec. and 140 in./sec. The oil-in-water emulsion formation temperature was 165.degree. F..+-.5.degree. F. The following Table V discloses the results of six (6) experimental runs:

The above data indicates that redispersable emulsions can be formed with a static mixer without the biopolymer xanthan, and at surfactant concentration levels below 8,571.4 PPM.

The surfactants for this Example were NP 40 and NP 100 in a 1:1 ratio, and DP 150 and DNP 150 in a 1:1 ratio. The aqueous phase was brine. The oil-in-water emulsions were formed with a 1/2 inch diameter static shearer and mixer embodied by FIGS. 4-7 or FIGS. 8-13. The surfactants used were subject to degradation over a long period under stress. If the surfactants are depleted by degradation, the oil-in-water emulsion may fail by either phase separation or by inversion into a water-in-oil emulsion. The following table illustrates that with the emulsifiers of this invention, such failure is by the phase separation mode and not by inversion:

The oil samples used for these investigations were Manatokan crude. The aqueous phase was brine having a pH of greater than about 5.0. The surface active agents used in the testing series were the following ethoxylated nonyl phenols (NP): T-DET-N-20 (i.e. NP 20), T-DET-N-40 (i.e. NP 40), and T-DET-N-100 (i.e. NP 100). Each of the ethoxylated NP emulsifying agent(s) includes a collection of ethoxylated NP compounds wherein the number of (CH.sub.2 --CH.sub.2 --O).sub.y repeat units or segments can vary from where y may have a value ranging from about 4 to about 1000. "T-DET" is a trademark of the Thompson-Hayward Chemical Corp., Kansas City, Mo. The respective ethoxylated nonyl phenols were purified of glycols by polyglycol separation. The emulsifying composition(s) was mixed with the Manatokan crude at a temperature of 125.degree. F..+-.25.degree. F. An oil-in-water (or oil-in-aqueous phase) emulsion was formed with the emulsifying-crude mixture by positioning the mixture in a rotor stator mixer. Mixing energies were 2,000 rpm to 4,000 rpm for 40 secs. to 80 secs. The oil-in-water emulsion(s) produced contained from about I5 percent to about 60 percent by weight brine. The following Table VIII discloses shear life (which is the measure of emulsion stability) that was detected for the various mixtures of NP 20/NP 40/NP100:

With the emulsifier(s) of this invention, failure by separation results in a slight decrease in fluid viscosity and permits continued pipeline operation. The pipe loop runs indicate that phase separation is the mode of transport emulsion failure for various crudes.

The surfactants for this Example were Triblock Pluronic plus tridecyl alcohol containing 150 moles ethylene oxide plus a biopolymer (other than xanthan). The aqueous phase was brine. Oil-in-water emulsion(s) were attempted to be formed with a 0.5 inch diameter Komax (FIGS. 8-13) or a dynamic mixer. The following Table VII illustrates that the oil-in-water emulsion(s) failed with the emulsifier(s) by inversion:

Assuming that for commercial purposes an emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying mixture in Table VIII producing an oil-in-water emulsion with an acceptable (i.e. commercially acceptable) emulsion shear stability is the 25/25/50 mixture of NP 20/NP 40/NP 100. The weight average molecular weight for this mixture was 2301 (which was between 1966 and 9188) and the dispersity of 1.77 was between 1.0 and 5.0. Furthermore, the estimated quantity in % by weight of NP compounds in the 25/25/50 surfactant mixture having a molecular weight of between 1966 and 9188 was 51% by weight (which is greater than at least 50% by weight). The 50/25/25 mixture did not produce an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the weight average molecular weight of the mixture was 1946 (which is not between 1966 and 9188), and further because the estimated quantity in % by weight of NP compounds in the 50/25/25 surfactant mixture having a molecular weight of 1966 to 9188 Was 41% by weight (which is less than at least 50% by weight). The 25/50/25 mixture also did not produce an acceptable oil-in-water emulsion because the estimated quantity in % by weight of NP compounds in the 25/50/25 surfactant mixture having a molecular weight of 1966 to 9188 was 37% by weight, which is less than 50% by weight. Had this estimated quantity in % by weight been 50% by weight or greater, an acceptable oil-in-water emulsion would have been formed.

The oil or hydrocarbon samples utilized for these investigations were Manatokan crude. The water or aqueous phase was brine with a pH of greater than about 4.5. The emulsifying agents were the following ethoxylated nonyl phenols (NP): T-DET-N-40 (i.e. NP 40), T-DET-N-100 (i.e. NP 100), and T-DET-N-150 (i.e. NP 150). Similar to the emulsifying agent(s) in Example XXIV, each of these ethoxylated NP emulsifying agent(s) includes a collection of ethoxylated nonyl phenol compounds wherein the number of ##STR40## repeat units of segments can vary from where y may have a value of from about 4 to about 1000. All emulsifying agent(s) were purified of glycols by polyglycol separation. From about 100 ppm to about 5000 ppm (typically about 750 ppm) of emulsifying agent(s) by weight of Manatokan crude were mixed with each other in various proportions by weight and with the aqueous phase brine to form emulsifying composition(s). The Manatokan crude was mixed with the emulsifying composition(s) at a temperature of 135.degree. F..+-. about 35.degree. F. An oil-in-water (or crude-in-water) emulsion was formed with the emulsifying-crude mixture by positioning the mixture in a rotor stator mixer. Mixing energies were 2,000 rpm to 4,000 rpm (typically 3,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) produced contained from about 15 percent to about 60 percent by weight aqueous phase (i.e. brine). The following Table IX discloses shear life (or emulsion stability) that was measured or discovered for the various mixtures of NP 40/ NP 100/NP 150:

All emulsifying mixtures produced a commercially acceptable (i.e. above 40 mins.) oil-in-water emulsion because for each mixture, the weight average molecular weights were between 1966 and 9188, the dispersities Were between 1.0 and 5.0, and the % by weight of NP compounds (in the emulsifying agent mixture) having a molecular weight between 1966 and 9188 was at least 50% by weight. Had any particular emulsifying mixture had a dispersity greater than about 5.0 and/or a weight average molecular weight outside of the range of 1966 to 9188 and/or less than about 50% by weight of the NP compounds in the emulsifying agent mixture having a molecular weight of 1966 to 9188, the formed oil-in-water emulsion produced therefrom would not have been commercially acceptable.

The oil samples are Manatokan crude. The aqueous phase is brine with a pH above 4.0. The emulsifying agent(s) are NP 30 (i.e. T-DET-N-30) and NP 270 (i.e. T-DET-N-270). Each NP emulsifying agent comprises a group or collection of ethoxylated nonyl phenol compounds wherein the (CH.sub.2 --CH.sub.2 --O).sub.y repeat units range from where y has a value of about 4 to about 1000. NP 30 and/or NP 270 has at least one ethoxylated alkylphenol compound having the general formula: ##STR41## where y is greater than 100, more typically greater than 100 but less than 1000, and the ethoxylated alkylphenol compound preferably comprises at least 1% by weight (more preferably 1% to 90% by weight) of the entire mixture of NP 30 and NP 270 together. The emulsifying agent(s) are purified from glycols. From 100 ppm to 5000 ppm of emulsifying agent(s) by weight of Manatokan crude are mixed with each other in an 80% NP 30/20% NP 270 proportion by weight and with the aqueous phase brine to form emulsifying composition(s). The Manatokan crude is mixed with the emulsifying composition(s) at a temperature of 110.degree. F..+-. about 10.degree. F. The mixture is placed in a rotor stator mixer and the latter is energized at a mixing energy between 2,000 rpm to 4,000 rpm for 40 to 60 secs. to form or produce oil-in-water emulsion(s) containing from about 15 percent to about 60 percent by weight aqueous phase (i.e. brine). The following Table X discloses emulsion stability that is found for the 80%/20% by weight mixture of NP 270:

The emulsifying mixture in this Example produces a commercially unacceptable oil-in-water emulsion. The reason for the unacceptable oil-in-water emulsion is that the estimated quantity in % by weight of NP compounds in the emulsifying mixture having a molecular Weight of 1966 to 9188 is 0%.

Repeat Example XXVI but for 60% by weight of NP 15 and 40% by weight NP 100 and find the following: a weight average molecular Weight of 3790 for the 60% NP 15/40% NP 100 mixture, a dispersity of 1.59, and 40% by weight as the estimated quantity of NP compounds in the 60% NP 15/40% NP 100 mixture having a molecular weight between 1966 and 9188, and an emulsion shear stability of 25 mins. or less. The emulsion shear stability is unacceptable because of the 40% by weight of the estimated quantity of NP compounds in the 60% NP 15/40% NP 100 mixture.

Repeat Example XXVI but for 45% by weight NP 10 and 55% by weight NP 50 and find the following: a weight average molecular weight of 1628 for the 45% NP 10/55% NP 50 mixture, a dispersity of 1.29, and 55% by weight as the estimated quantity of NP compounds in the 45% NP 10/55% NP 50 mixture having a molecular weight between 1966 and 9188, and an emulsion shear stability of less than 10 mins. The emulsion shear stability is unacceptable because of the 1628 weight average molecular weight.

Repeat Example XXVI but for 60% by weight NP 150 and 40% by weight NP 300 and find the following: a weight average molecular weight of 10,565 for the 60% NP 150/40% NP 300 mixture, a dispersity of 1.12, and 60% by weight as the estimated quantity of NP compounds in the 60% NP 150/40% NP 300 mixture having a molecular weight between 1966 and 9188, and an emulsion shear stability of less than 35 mins. The emulsion shear stability is unacceptable because of the 10,565 weight average molecular weight.

Repeat Example XXVI but for 90% by weight NP 100 and 10% by weight NP 1000 and find the following: a weight average molecular weight of 15,900 of the 90% NP 100/10% NP 1000 mixture, a dispersity of 2.19, and 90% by weight as the estimated quantity of NP compounds in the 90% NP 100/10% NP 1000 mixture having a molecular weight between 1966 and 9188, and an emulsion shear stability of less than 35 mins. The emulsion shear stability is unacceptable because of the 15,900 weight average molecular weight.

The oil samples for these investigations are Manatokan crude. The aqueous phase is brine having a pH of greater than about 5.0. The surface active agents in the testing series are the following ethoxylated nonyl phenol compounds: T-DET-N-10.5 (i.e. NP 10.5), T-DET-N-20 (i.e. NP 20), and T-DET-N-30 (i.e. NP 30). Each of the ethoxylated NP emulsifying agent(s) includes a collection of ethoxylated NP molecules wherein the number of (CH.sub.2 --CH.sub.2 --O).sub.y repeat units or segments can vary from where y may have a value ranging from about 4 to about 200. "T-DET" is a trademark of the Thompson-Hayward Chemical Corp., Kansas City, Mo. The respective ethoxylated nonyl phenols are purified of polyethylene glycol by polyethylene glycol separation. The emulsifying composition(s) is mixed with the Manatokan crude at a temperature of 125.degree. F..+-.25.degree. F. An oil-in-water (or oil-in-aqueous phase) emulsion is formed in some instances with the emulsifying-crude mixture by positioning and agitating the mixture in a rotor stator mixer. Mixing energies are 500 rpm to 4,000 rpm (typically 1,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) that are produced contain from about 15 percent to about 60 percent by weight brine. The following Table XI discloses time to form a water continuous emulsion and shear life of the water continuous emulsion after formation (which is the measure of emulsion stability) that is detected for the various mixtures of NP 10.5/NP 20/NP 30:

Assuming that for commercial purposes a period of time greater than about 20 secs. to form a water continuous emulsion is unacceptable and a water continuous emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying mixture in Table XII producing an oil-in-water emulsion within an acceptable period of time and with an acceptable (i.e. commercially acceptable) emulsion shear stability is the 60/20/20 mixture of NP 10.5NP 20/NP 30. The weight average molecular weight for this mixture is 1220 (which is between 558 and 2405) and the dispersity of 1.70 is between 1.0 and 5.0. Furthermore, the estimated quantity in percent by weight of NP compounds in the 20/60/20 surfactant mixture having a molecular weight of between 558 and 2504 is 85% by weight (which is greater than at least 50% by weight). The 60/20/20 mixture did not produce within an acceptable period of time of less than about 20 secs. an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the estimated quantity in percent by weight of NP compounds in the 60/20/20 surfactant mixture having a molecular weight 558 to 2504 is 37% by weight (which is less than at least 50% by weight). The 20/20/60 mixture also did not produce an acceptable oil-in-water emulsion because the estimated quantity in percent by weight of NP compounds in the 20/20/60 surfactant mixture having a molecular weight of 558 to 2504 is 42% by weight, which is less than 50% by weight. If this estimated quantity in percent by weight is 50% by weight or greater, an acceptable oil-in-water emulsion would be formed within an acceptable period of time.

The oil or hydrocarbon samples for these investigations are Manatokan crude. The water or aqueous phase is brine having a pH of greater than about 4.5. The emulsifying agents are the following ethoxylated nonyl phenol compounds: T-DET-N-20 (i.e. NP 20), T-DET-N-40 (i.e. NP 40), and T-DET-N-70 (i.e. NP 70). Similar to the emulsifying agent(s) in Example XXXI, each of the ethoxylated NP emulsifying agent(s) includes a collection of ethoxylated nonyl phenol molecules wherein the number of (CH.sub.2 --CH.sub.2 --O).sub.y repeat units or segments can vary from where y may have a value of from about 4 to about 200. All emulsifying agent(s) are purified of polyethylene glycol by polyethylene glycol separation. From about 100 ppm to about 5,000 ppm (typically about 750 ppm) of emulsifying agent(s) by weight of Manatokan crude are mixed with each other in various proportions by weight and with the aqueous phase brine to form emulsifying composition(s). The Manatokan crude is mixed with the emulsifying composition(s) at a temperature of 135.degree. F..+-. about 25.degree. F. An oil-in-water (or crude-in-water) emulsion is formed in some instances with the emulsifying-crude mixture by positioning and agitating the mixture in a rotor stator mixer. Mixing energies are 500 rpm to 4,000 rpm (typically 1,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) that are produced contain from about 15 percent to about 60 percent by weight aqueous phase (i.e. brine). The following Table XII discloses time to form a water continuous emulsion and shear life of the water continuous emulsion after formation (or emulsion stability) that is measured or discovered for the various mixtures of NP 20/NP 40/NP 70:

Assuming that for commercial purposes a period of time greater than about 20 secs. to form a water continuous emulsion is unacceptable and a water continuous emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying mixture in Table XII producing an oil-in-water emulsion within an acceptable period of time and with an acceptable (i.e. commercially acceptable) emulsion shear stability is the 60/20/20 mixture of NP 20/NP 40/NP 70. The weight average molecular weight for this mixture is 2230 (which is between 558 and 2504) and the dispersity of 1.20 is between 1.0 and 5.0. Furthermore, the estimated quantity in percent by weight of NP compounds in the 60/20/20 surfactant mixture having a molecular weight of between 558 and 2504 is 70% by weight (which is greater than at least 50% by weight). The 20/20/60 mixture did not produce within an acceptable period of time of less than about 20 secs. an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the weight average molecular weight of the mixture is 3020 (which is not between 558 and 2504), and furthermore because the estimated quantity in percent by weight of NP compounds in the 20/20/60 surfactant mixture having a molecular weight of 558 to 2504 is 40% by weight (which is less than at least 50% by weight). The 20/60/20 mixture also did not produce an acceptable oil-in-water emulsion because the estimated quantity in percent by weight of NP compounds in the 20/60/20 surfactant mixture having a molecular weight of 558 to 2504 is 47% by weight, which is less than 50% by weight. If this estimated quantity in percent by weight is 50% by weight or greater, an acceptable oil-in-water emulsion would be formed within an acceptable period of time.

The oil samples for these investigations are Manatokan crude. The aqueous phase is brine having a pH of greater than about 5.0. The surface active agents in the testing series are the following ethoxylated nonyl phenol compounds: T-DET-N-5 (i.e. NP 5), T-DET-N-10.5 (i.e. NP 10.5), and T-DET-N-20 (i.e. NP 20). Each of the ethoxylated NP emulsifying agent(s) includes a collection of ethoxylated NP molecules wherein the number of ##STR42## repeat units or segments can vary from where y may have a value ranging from about 4 to about 200. The respective ethoxylated nonyl phenols are purified of polyethylene glycol by polyethylene glycol separation. The emulsifying composition(s) are mixed with the Manatokan crude at a temperature of 125.degree. F..+-.25.degree. F. An oil-in-water (or oil-in-aqueous phase) emulsion is formed with the emulsifying-crude mixture by positioning the mixture in a rotor stator mixer. Mixing energies are 520 rpm to 4,000 rpm (typically 1,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) that are produced contain from about 15 percent to about 60 percent by weight brine. The following Table XIII discloses time to form a water continuous shear life of the water continuous emulsion after formation (which is the measure of emulsion stability) that is detected for the various mixtures of NP 5/NP 10.5/NP 20:

Assuming that for commercial purposes a period of time greater than about 20 secs. to form a water continuous emulsion is unacceptable and a water continuous emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying mixture in Table XIII producing an oil-in-water emulsion within an acceptable period of time and with an acceptable (i.e. commercially acceptable) emulsion shear stability is the 20/20/60 mixture of NP 5/NP 10.5/NP 20. The weight average molecular weight for this mixture is 1010 (which is between 558 and 2504) and the dispersity of 1.16 is between 1.0 and 5.0. Furthermore, the estimated quantity in percent by weight of NP compounds in the 20/20/60 surfactant mixture having a molecular weight of between 558 and 2504 is 77.6% by weight (which is greater than at least 50% by weight). The 60/20/20 mixture did not produce an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the estimated quantity in percent by weight of NP compounds in the 60/20/20 surfactant mixture having a molecular weight of 558 to 2504 is 39.1% by weight (which is less than at least 50% by weight). The 20/60/20 mixture also did not produce an acceptable oil-in-water emulsion because the estimated quantity in percent by weight of NP compounds in the 20/60/20 surfactant mixture having a molecular weight of 558 to 2504 is 45% by weight, which is less than 50% by weight. If this estimated quantity in percent by weight is 50% by weight or greater, an acceptable oil-in-water emulsion would be formed.

Repeat Example XXXI with the emulsifying composition(s) mixed with the Manatokan crude at a temperature of about 185.degree. F., and find that the 20/60/20 mixture of NP 10.5/NP 20/NP 30 did not produce an oil-in-water emulsion within a commercially acceptable period of time and with a commercially acceptable emulsion shear stability because the emulsifying composition(s)-Manatokan crude had a temperature above about 170.degree. F.

Repeat Example XXXII with the emulsifying composition(s) mixed with the Manatokan crude at a temperature of about 180.degree. F., and find that the 60/20/20 mixture of NP 20/NP 40/NP 70 did not produce an oil-in-water emulsion within a commercially acceptable period of time and with a commercially acceptable emulsion shear stability because the emulsifying compositions-Manatokan crude had a temperature above about 170.degree. F.

Repeat Example XXXIII with the emulsifying composition(s) mixed with the Manatokan crude at a temperature of about 195.degree. F., and find that the 20/20/60 mixture of NP 5/NP 10.5/NP 20 did not produce an oil-in-water emulsion within a commercially acceptable period of time and with a commercially acceptable emulsion shear stability because the emulsifying composition(s)-Manatokan crude had a temperature above about 170.degree. F.

The oil samples are Manatokan crude. The aqueous phase is brine with a pH above 4.0. The emulsifying agent(s) comprise 75% by weight ethoxylated nonyl phenols (NP) agents and 25% by weight of at least one ethoxylated alkylphenol (EA) agent having the general formula: ##STR43## where n is an integer having a value of from 9 to 14 (inclusive) and y is an integer having a value of from 4 to 300 (inclusive). The EA agent has a molecular weight distribution with a dispersity of from about 1.0 to about 5.0 and with a weight average molecular weight of from about 2434 to about 4264; and at least about 50% by weight of the EA agent comprises at least one ethoxylated alkylphenol compound having a molecular weight of from about 2434 to about 4264. The NP agents are the following: T-DET-N 20 (i.e. NP 20), T-DET-N 40 (i.e. NP 40,:, and T-DET-N 100 (i.e. NP 100). Each of the ethoxylated NP agents includes a collection of ethoxylated NP compounds wherein the number of (CH.sub.2 --CH.sub.2 --O).sub.y repeat units or segments can vary from where y may have a value ranging from about 4 to about 200. All of the respective emulsifying agents are purified of glycols by polyglycol separation. From about 100 ppm to about 5,000 ppm (typically about 750 ppm) of the emulsifying agent(s) by weight of Manatokan crude are mixed with each other in various proportions by weight and with the aqueous phase brine to form emulsifying composition(s). The Manatokan crude is mixed with the emulsifying composition(s) at a temperature of 190.degree. F..+-.5.degree. F. An oil-in-water (or oil-in-aqueous phase) emulsion is formed with the emulsifying composition-crude mixture by positioning the mixture in a rotor stator mixer. Mixing energies are 2,000 rpm to 4,000 rpm (typically 3,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) that are produced contain from about 15% to about 60% by weight aqueous phase (i.e. brine). The following Table XIV discloses time to form a water continuous emulsion and shear life (or emulsion stability) that is measured or discovered for the various mixtures of NP 20/NP 40/NP 100 in combination with the 25% by weight of the EA agent:

Assuming that for commercial purposes a period of time greater than about 20 secs. to form a water continuous emulsion is unacceptable and a water continuous emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying NP/EA agent mixture in Table XIV producing an oil-in-water emulsion within an acceptable period of time and with a commercially acceptable emulsion shear stability is the 45/15/15 mixture of NP 20/NP 40/NP 100 in combination with 25% by weight EA agent. The weight average molecular weight for the NP mixture is 1284 (which is between 558 and 1582) and the dispersity of 1.52 is between 1.0 and 5.0. Furthermore, the estimated quantity in % by weight of NP compounds in the NP mixture having a molecular weight of between 558 and 1582 is 67% by weight (which is greater than at least 50% by weight). The 15/45/15 mixture of NP 20/NF 40/NP 100 in combination with 25 % by weight of the EA agent did not produce within an acceptable period of time of less than about 20 secs. an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the estimated quantity in percent by weight of NP compounds in the NP mixture having a molecular weight of 558 to 1582 is 37% by weight (which is less than at least 50% by weight). If this estimated quantity in percent by weight is 50% by weight or greater, an acceptable oil-in-water emulsion would be formed within an acceptable period of time. The 15/15/45 mixture of NP 20/NP 40/NP 100 in combination with 25% by weight of the EA agent did not produce an acceptable oil-in-water emulsion because the estimated quantity in percent by weight of NP compounds in the 15/15/45 NP mixture having a molecular weight of 558 to 1582 is 22.I% by weight (which is less than at least 50% by weight), and further because the weight average molecular weight of the mixture is 2753 (which is not between 558 and 1582). If this estimated quantity in percent by weight is 50% by weight or greater and if the weight average molecular weight is between 558 and 1582, an acceptable oil-in-water emulsion would be formed within an acceptable period of time.

Repeat Example XXXVII where n in the general formula: ##STR44## is 8 or less and find that an acceptable oil-in-water emulsion is not formed and/or is not formed within an acceptable period of time.

Repeat Example XXXVII where n in the general formula: ##STR45## is 15 or greater and find that an acceptable oil-in-water emulsion is not formed and/or is not formed within an acceptable period of time.

Repeat Example XXXVII where the percent by weight of the EA agent in the NP/EA agent mixture is decreased to below 15% by weight and the percent by weight of the respective NP compounds (i.e. NP 20, NP 40, and NP 100) in the NP/EA agent mixture is varied and/or adjusted accordingly such that the weight average molecular weight of the NP mixture is 558 to 1582, dispersity of the NP mixture is 1.0 to 5.0, and the estimated quantity in percent by weight of NP compounds in the NP mixture having a molecular weight between 558 and 1582 is at least 50% by weight, and find that an acceptable oil-in-water emulsion is not formed and/or is not formed within an acceptable period of time.

Repeat Example XXXX where the percent by weight of the EA agent in the NP/EA agent mixture is increased above 40% by weight and find similar results.

The oil samples are PCEJ crude. The aqueous phase is brine with a pH above 4.5. The emulsifying agent(s) comprise 75% by weight of an NP 20 agent and 25% of three ethoxylated alkylphenol agents with each of the agents having the general formula: ##STR46## wherein for one agent (hereinafter identified as DD 20) y equals 20 and is a mean of a normal (Gaussian) distribution curve; for a second agent (hereinafter identified as DD 70) y equals 70 and is a mean of a normal (Gaussian) distribution curve; and for the third agent (hereinafter identified as DD 150) y equals 150 and is also a mean of a normal (Gaussian) distribution curve. The mixture of DD 20/DD 70/DD 100 will be referred to collectively hereafter as the DD mixture. Each of the DD agents includes a collection of ethoxylated dodecyl compounds wherein the number of (CH.sub.2 --CH.sub.2 --O).sub.x repeat units or segments can vary from where x may have a value ranging from about 4 to about 300. The NP 20 agent has a molecular weight distribution with a dispersity of from about 1.0 to about 5.0 and with a weight average molecular weight of from about 558 to about 1582; and at least about 50% by weight of the NP 20 agent comprises at least one ethoxylated nonyl phenol compound having a molecular weight of from about 558 to about 1582. All of the respective emulsifying agents are purified of polyethylene glycols by polyethylene glycol separation. From about 100 ppm to about 5,000 ppm (typically about 750 ppm) of the emulsifying agent(s) by weight of PCEJ crude are mixed with each other in various proportions by weight and with the aqueous phase brine to form emulsifying composition(s). The PCEJ crude is mixed with the emulsifying composition(s) at a temperature of 200.degree. F..+-.5.degree. F. An oil-in-water (or oil-in-aqueous phase) emulsion is formed with the emulsifying composition-crude mixture by positioning, placing or passing the mixture through a rotor stator mixer. Mixing energies are 2,000 rpm to 4,000 rpm (typically 3,000 rpm) for 30 secs. to 90 secs. The oil-in-water emulsion(s) that are produced contain from about 15 percent to about 60 percent by weight aqueous phase (i.e. brine). The following Table XV discloses time to form a water continuous emulsion and shear life (or emulsion stability) that is measured or discovered for the various mixtures of DD 20/DD 70/DD 150 in combination with the 75% by weight of the NP 20 agent:

Assuming that for commercial purposes a period of time greater than about 20 secs. to form a water continuous emulsion is unacceptable and a water continuous emulsion shear stability of less than 40 mins. is unacceptable, the only emulsifying DD/NP 20 mixture in Table XV producing an oil-in-water emulsion within an acceptable period of time and with a commercially acceptable emulsion shear stability is the 5/15/5 mixture of DD 20/DD 70/DD I50 in combination with 75% by weight NP 20 agent. The weight average molecular weight for the DD mixture is 4171 (which is between 2434 and 4264) and the dispersity of 1.30 is between 1.0 and 5.0. Furthermore, the estimated quantity in percent by weight of DD compounds in the DD mixture having a molecular weight of between 2434 and 4264 is 55% by weight (which is greater than at least 50% by weight). The 15/5/5 mixture of DD 20/DD 70/DD 150 in combination with 75% by weight percent of the NP 20 agent did not produce within an acceptable period of time of less than about 20 secs. an acceptable oil-in-water emulsion having an emulsion shear stability greater than or equal to 40 mins. because the estimated quantity in percent by weight of DD compounds in the DD mixture having a molecular weight of 2434 to 4264 is 16.4% by weight (which is less than at least 50% by weight). If this estimated quantity in percent by weight is 50% by weight greater, an acceptable oil-in-water emulsion would be formed within an acceptable period of time. The 5/5/15 mixture of DD 20/DD 70/DD 150 in combination with 25% by weight of the NP 20 agent did not produce an acceptable oil-in-water emulsion because the estimated quantity in percent by weight of DD compounds in the 5/5/15 DD mixture having a molecular weight of 2434 to 4264 is 24% by weight (which is less than at least 50% by weight), and further because the weight average molecular weight of the mixture is 6281 (which is not between 2434 and 4264). If this estimated quantity in percent by weight is 50% by weight or greater and if the weight average molecular weight is between 2434 and 4264, an acceptable oil-in-water emulsion would be formed within an acceptable period of time.

Repeat Example XXXXII where the percent by weight of the NP 20 agent in the DD/NP 20 agent mixture is decreased to below about 60% by weight and the percent by weight of the respective DD compounds (i.e. DD 20, DD 70, and DD 100) in the DD/NP 20 agent mixture is varied and/or adjusted accordingly such that the weight average molecular weight of the DD mixture is 2434 and 4264, dispersity of the NP mixture is 1.0 to 5.0, and the estimated quantity in percent by weight of DD compounds in the DD mixture having a molecular weight between 2434 and 4264 is at least 50% by weight, and find that an acceptable oil-in-water emulsion is not formed and/or is not formed within an acceptable period of time.

Repeat Example XXXXIII where the percent by weight of the NP 20 agent in the DD/NP 20 agent mixture is increased above 85% by weight and find similar results.

The emulsifying agent for this Example is the emulsifying agent of Example XXXXII comprising the 5/15/5 mixture of DD 20/ DD 70/DD 150 in combination with 75% by weight NP 20 agent. The emulsifying agent is mixed with an aqueous phase (e.g. brine) at a temperature of about 200.degree. F. to form an emulsifying composition with the emulsifying agent comprising from about 5% by weight to about 60% by weight of the emulsifying composition. From about 2,000 to about 60,000 gallons of this emulsifying composition at a temperature of about 200.degree. F. is injected into a heavy crude or tar sands formation via an injection or production well over a period of one to five days. The formation has a temperature of about 190.degree. F. Subsequently, steam (75% to 100% quality) at 500.degree. F. is injected into the formation for a period of 20 to 40 days at a rate of 600 to 1,500 barrels per day. The production well is thereafter shut in for one to ten days to allow the steam and emulsifying composition to soak in the formation. Subsequently, the production well is opened up and production of oil-in-aqueous phase emulsion is started with the assistance of a downhole pump at the bottom of the production well.

Repeat Example XXXXV but concurrently inject into the formation at a rate of about 1,000 barrels per day the emulsifying composition with the 500.degree. F. steam such that the emulsifying composition enters into the formation at a temperature above P.I.T. (or about 210.degree. F.) and the weight ratio of the 500.degree. F. steam to the emulsifying composition is about 20:1. The weight ratio of the steam to emulsifying composition can vary from about 1:1 to about 50:1, and hot water having a temperature of 150.degree. F. to 250.degree. F. or hot water and steam can be substituted for the steam in the same weight ratio. After shutting in the production well for a soak period of 10 to 20 days wherein the emulsifying composition cools to below about P.I.T. (or about 210.degree. F.) and oil-in-aqueous phase emulsion forms, the production well is opened up and the oil-in-aqueous phase emulsion is produced having a greater or enhanced stability than the oil-in-aqueous phase emulsion of Example XXXXV.

The oil samples used for this investigation was a sour vacuum residuum with a nominal 1000 deg. F. plus TBP cut point and which was obtained from produced crude oil having been refined initially through an atmospheric distiller where the atmospheric bottoms were recovered and subsequently refined through a vacuum distiller to produce the sour vacuum residuum from the bottom thereof. The aqueous phase was water. The emulsifying agent(s) included at least one ethoxylated alkylphenol compound having the general formula: ##STR47## wherein n.sub.1 is an integer having a value of from about 7 to about 20, and y.sub.1 is an integer having a value of from about 4 to about 1000; and the at least one ethoxylated alkylphenol compound has a molecular weight distribution with a dispersity of from about 1.0 to about 5.0 and with a weight average molecular weight of from about 1966 to about 9188; and wherein at least about 50% by weight of the emulsifying agent comprises the at least one ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188. From 1% by weight to 90% by weight of the emulsifying agent(s) comprises the at least one ethoxylated alkylphenol compound wherein y.sub.1 has a value greater than 100. The sour vacuum residuum was heated to a temperature of about 225.degree. F. The emulsifying agent(s) and the water were commingled to form an emulsifying composition which was subsequently heated to a temperature of about 225.degree. F. The heated vacuum residuum and the heated emulsifying composition were pumped and admixed to form a heated mixture and the heated mixture was admitted into a 1/2 inch diameter static mixer with 16 mixing elements at an inlet pressure of from about 180 p.s.i. to about 260 p.s.i, more specifically about 255 p.s.i.g. and a flow rate of about 3.5 gpm. The resultant static mixer pressure differential was about 235 p.s.i. and the outlet pressure of the heated mixture was about 20 p.s.i.g.).

An oil-in-aqueous phase emulsion exited the static mixer with a pressure of about 20 p.s.i.g. and a temperature of about 225.degree. F. The produced emulsion, which comprised about 70 wt. % residuum, about 29.6 wt. % water and about 0.4 wt. % emulsifying agent(s), was subsequently depressurized to atmospheric pressure and was cooled to about 120.degree. F. within 5 mins. of formation. The formed emulsion had a stability (i.e. a shear life stability) of 3 hours. At the about 120.degree. F. temperature, the viscosity was about 185 cp. and the oil droplet size of the oil droplets are distributed such that about 50% of the residuum was contained in oil droplets of less than about 15 micron diameter and the ratio of the volume mean diameter (which may be defined as oil droplet diameter below which 50% of the oil volume in the sample exists) to the population mean diameter (which may be defined as oil droplet diameter below which half the number of oil droplets in the sample exists) was about 2.8. The produced emulsion can be subsequently burned in a process boiler designed to operate on No. 6 fuel oil.

Repeat Example XXXXVII above with the emulsifying agent(s) comprising a 50:50 mixture of NP-40 and NP-100 (i.e. the surface active agents of Example I) and find similar results.

Repeat Examples XXXXVII and XXXXVIII but with the temperature of the heated mixture (i.e. the heated vacuum residua and the heated emulsifying composition(s)) being 201.degree. F. or above and find similar results.

Repeat Examples XXXXVII, XXXXVIII and XXXXIX but with the hydrocarbon being atmospheric residua with a TBP above about 650.degree. F. and find similar results.

Repeat Examples XXXXVII, XXXXVIII, XXXXIX and XXXXX but with the static mixer having 32 baffle elements and a static mixer pressure differential of from about 180 p.s.i. to about 260 p.s.i.; and find a stability (i.e. a shear life stability) of 5 hours. Thus, it has been discovered that a static mixer with 32 baffle elements and with a static mixer pressure differential of from about 180 p.s.i. to about 260 p.s.i. and a flow rate of about 2.5 gpm produces an oil-in-aqueous phase emulsion with improved stability (i.e. improved shear life) when compared with an oil-in-aqueous phase emulsion produced in a static shearing and mixing device having 16 baffle elements and with the same static mixer pressure differential of from about 180 p.s.i. to about 260 p.s.i., especially when the hydrocarbon has a nominal TBP cut point exceeding a temperature of about 650.degree. F. and above (e.g. asphalt residua), more preferably when the hydrocarbon has a nominal TBP cut point exceeding a temperature of about 950.degree. F. and above (e.g. a vacuum residua).

The oil samples used for this investigation was crude bitumen (i.e. bitumen from Athabasca tar sands). The aqueous phase was water. The emulsifying agent(s) included at least one ethoxylated alkylphenol compound having the general formula: ##STR48## wherein n.sub.1 is an integer having a value of from about 7 to about 20, and y.sub.1 is an integer having a value of from about 4 to about 1000; and the at least one ethoxylated alkylphenol compound has a molecular weight distribution with a dispersity of from about 1.0 to about 5.0 and with a weight average molecular weight of from about 1966 to about 9188; and wherein at least about 50% by weight of the emulsifying agent comprises the at least one ethoxylated alkylphenol compound having a molecular weight of from about 1966 to about 9188. From 1% by weight to 90% by weight of the emulsifying agent(s) comprises the at least one ethoxylated alkylphenol compound wherein y.sub.1 has a value greater than 100. The bitumen contained about 2.5% by wt. water and was heated to a temperature of about 235.degree. F. The emulsifying agent(s) and the water were commingled to form an emulsifying composition which was subsequently heated to a temperature of about 184.degree. F. The heated bitumen and the heated emulsifying composition were pumped at a rate of 2.5 gal./min. and 1.1 gal./min. respectively and admixed to form a heated mixture and the heated mixture was admitted into a 1/2 inch diameter static mixer with 8 mixing elements at an inlet pressure of from about 50 p.s.i. to about 260 p.s.i, more specifically about 85 p.s.i.g. and a flow rate of about 3.6 gpm. The resultant static mixer pressure differential was about 65 p.s.i. and the outlet pressure of the heated mixture was about 20 p.s.i.g.

An oil-in-aqueous phase emulsion exited the static mixer with a pressure of about 20 p.s.i.g. and a temperature of about 210.degree. F. The produced emulsion, which comprised about 68 wt. % bitumen, about 31.9 wt. % water and about 0.1 wt. % emulsifying agent(s), was subsequently depressurized to atmospheric pressure and was cooled to about 120.degree. F. within 5 mins. of formation. The formed emulsion had a stability (i.e. a shear life stability) of 21/2 hrs. At the about 120.degree. F. temperature, the viscosity was about 200 c.p. and the oil droplet size of the oil droplets are distributed such that about 50% of the bitumen was contained in oil droplets of less than about 26 micron diameter and the ratio of the volume mean diameter (which may be defined as oil droplet diameter below which 50% of the oil volume in the sample exists) to the population mean diameter (which may be defined as oil droplet diameter below which half the number of oil droplets in the sample exists) was about 3.5. The produced emulsion can be subsequently burned in a process boiler designed to operate on No. 6 fuel oil.

Repeat Example XXXXXII above with the emulsifying agent(s) comprising a 50:50 mixture of NP-40 and NP-100 (i.e. the surface active agents of Example I) and find similar results.

Asphalt emulsion fuel samples with very desirable properties were made in both a Batch Emulsion Preparation Unit (BEPU) and a Continuous Emulsion Preparation (CEP) unit. Operation of the CEP unit on asphalt, a nominal 1050.degree. F. plus vacuum resid., was excellent. Properties of the asphalt used are shown in Table XVI. A summary of results for runs using uncut Sinclair sour AC-20 asphalt is given in Table XVII. An excellent emulsion was CEP-109-6, which is adequately fine and narrow in particle size distribution (PSD), such that there was no congealed sediment. Dynamic stability and static stability of the produced emulsions were excellent. Viscosity of 141 cp at 120.degree. F. was surprisingly attractive for such a finely dispersed emulsion, attributable in part to very minimal inclusion of water in the internal phase. Three drums of asphalt--based Water Continuous Emulsion (WCE) fuel were produced in runs CEP-110 and 111, for use in burn testing in a tunnel furnace. The three drums were prepared at the following operating conditions derived from test CEP 109-6:

The standard water content of about 30% by wt. was ideal for the desired spray viscosity of around 100 cp at 120.degree. F. Results show that much richer asphalt emulsions can be prepared, and can possess very good static storage stability. These have heavy consistency from thick liquid to heavy paste. The preferred range of water content for asphalt emulsion fuels was 27-33% by wt. with a wider range 20-40% by wt. also being acceptable. Concentrates for storage or shipping can be made as low as about 10% by wt. water.

A preferred operating temperature was from about 205.degree. F. to about 215.degree. F., more preferably about 210.degree. F. Lower temperatures resulted in coarser emulsions due to higher asphalt viscosity. Higher temperatures for this Example could possibly result in diminished surfactant effectiveness. CEPI10-4 and CEPIIl-1 showed that emulsion formation at temperatures of 225.degree. F. and higher could result in higher oversize content, more skim formation, poorer static stability and poorer dynamic stability.

The acceptable range of oil and aqueous phase mix temperatures was about 160.degree. and about 230.degree. F. respectively, preferably about 205.degree. and about 215.degree. F. respectively. Either the oil or water may be higher than the mix temperature, but system backpressure must be maintained sufficient at all points to suppress incipient flashing (formation of vapor bubbles).

Surfactant type used in this Example was a 50/50 mix of NP40/NP100, the same as used in heavy-crude transport emulsions, and the technical description of surfactant types applicable to asphalt WCE fuel formation was identical to that for transport emulsions. It was anticipated that a useful range was about 500 to about 5000 ppm in emulsion, preferably about 1000 to about 2000 ppm. Thickeners such as xanthan gum and/or co-surfactants could be used to increase stability.

Best emulsions were produced using 32 mixer elements (Komax). This results in finer, narrower particle size distributions than with fewer elements, giving increased emulsion static stability. If 32 elements were not used in Komax-type mixers, the result was an emulsion with wider particle size distribution and thus more oversize material, as seen in comparing runs CEP108 and CEP109. The wider PSD emulsions are less stable. Runs in the BEPU unit show that no effective emulsion was formed at all using 8 elements in Komax-type mixers.

All of the asphalt emulsions produced with 30-percent water fall within a relatively narrow range of viscosity, typically 130-150 cp at 120.degree. F. The variation with temperature was much less sensitive than for oils or heavy crude emulsions, as shown in FIG. 21. As with other WCE's, decreasing the water content causes an increased viscosity, for example, the run BEPU-21 emulsion at 25% water had a viscosity of 309 cp.

As shown in Table XVIII, static storage stability of good asphalt emulsions such as CEP109-4, CEP109-6, CEPIIl-3 and CEPIIl-6X was quite good, and there was not much tendency to form additional congealed material after initial cooling of the emulsion. The initial screenings of the emulsions show significantly more oversize than was formed during prolonged static storage. Dynamic stabilities were also excellent on the good emulsions, but poor in this Example on the emulsions produced at temperatures above 225.degree. F. In order to achieve best static and dynamic stabilities, emulsions should be produced below about 225.degree. F., preferably 205.degree.-215.degree. F. for this particular asphalt grade. Also, particle size should be kept small and narrowly distributed, for example volumetric mean particle diameter of about 29 microns, d.sub.50 of about 20 microns and dispersity of about 3 to 3.5. The term "d.sub.50 " particle size may be defined as the droplet size at which half the total oil is in the form of larger droplets (i.e. larger than 20 microns) and half in the form of smaller droplets (i.e. smaller than 20 microns).

A one-quart sample of a fair-quality asphalt fuel emulsion, CEP108-2, was subjected to gentle stirring at room temperature for one month, using a 45 mm diameter turbine stirrer at 90 rpm. This test comparatively simulated dynamic stress such as that experienced by the emulsion in pipeline flow. Results of the test, shown in Table XIX, indicate a very gradual particle size degradation, with the emulsion still quite good after 32 days, excepting the formation of 14.8% by wt. oversize material. This formation of oversize material is typical in extended pipeline flow. It is believed this material would likely perform very well in pipeline transport, especially considering that the starting emulsion sample was not formed at optimum conditions.

A water-cooled heat exchanger was incorporated into the CEP unit to cool asphalt emulsions below boiling temperature prior to discharge. Heat transfer data for this cooler are given in Table XX. Heat transfer is limited by convective heat transfer on the emulsion side, which is in laminar flow, thus the h-values were calculated only for the emulsion side. These results show that no gradual degradation of the heat transfer efficiency is apparent and that higher-than-expected heat transfer was observed, especially in asphalt-emulsion runs. No cooling at all was observed in run CEPIIIB. It is concluded that gross fouling of the exchanger with asphalt occurred between runs 111A and 111B, due to operating procedure which apparently allowed asphalt emulsion to remain stagnant in steam-traced lines, causing asphalt separation and subsequent migration onto cold exchanger surfaces.

Quenching of asphalt emulsion prior to storage is more preferred to maintain maximum emulsion stability. Normally, a small quantity of asphalt-foam skim forms on top of the produced material. Preferably, about 1% by wt. (or less) of the produced emulsion is asphalt-foam skim. Asphalt-foam skim can be removed by skimming and recycled (continuously) to be admixed with the emulsifying composition and/or hydrocarbon to form the emulsion. Quenching minimizes and/or prevents and/or retards the skim. The about 2% by wt. skim formed in run 111B was due to ineffectiveness of the quench. It has been observed that skim formation is worse when oversize content is higher, and worse when temperature is higher. It has been further observed that skim formation is effected by presence of vapor bubbles in the emulsion. Higher-temperature runs, such as at 225.degree. F. or above could work better if artificial backpressure is exerted against the cooler outlet, to prevent microbubbles in the water phase due to incipient flashing between the mixer outlet and cooler inlet.

The results in this Example were based on a single resid feed material. If the feedstock was varied, the emulsion formation operating conditions should be adjusted accordingly. In particular, if the resid viscosity is varied, the mixing temperature and/or mixing energy input should be adjusted to obtain the desirable particle size distribution.

Repeat Example XXXXVII and burn the produced emulsion in a boiler to generate steam. About 50,000 BPD steam is sent to an in situ production operation where Athabasca tar sands are mixed with the steam to produce 10,000 BPD bitumen having an API gravity of about 10.8.degree. API. The bitumen was subsequently heated to a temperature of about 200.degree. F. and subsequently refined through an atmospheric still and then through a vacuum still. 5600 BPD of light crude fraction (@ 1050.degree. F., 19.6.degree. API, viscosity 350 c.p. @ 60.degree. F.) was produced and recovered in the overhead from both the atmospheric still and the vacuum still. The sour vacuum residuum with a nominal 1000 deg. F. plus TBP cut point was recovered from the vacuum distillator and recycled to produce the produced emulsion.

An asphalt fuel emulsion was prepared with the hydrocarbon and emulsifying composition of Example XXXXVII and in accordance with the procedure of Example XXXXVII. Over a long period of time (say from 1 hour to 8 weeks or longer) asphalt fuel emulsion is subject to sedimentation in static storage. After six (6) weeks of static storage in a drum, the asphalt emulsion fuel contained a thick paste layer of several inches on the bottom. This thick paste layer may be redispersed into the asphalt emulsion fuel by mixing or otherwise agitating.

Several means of enhancing static stability (reducing sedimentation) of asphalt fuel emulsions were tested including use of polymer additives, further reduction of particle size, use of additional surfactant, and storage at reduced water content. Sedimentation rate is characterized by a long term static stability test, in which the viscosity of the sample was measured as a function of depth within the sample. A heavily sedimented sample shows a strong increase in viscosity toward the bottom, whereas a non-sedimented sample exhibits uniform viscosity. Generally the severity of sedimentation increases with time. The results of screening several additives are shown in FIG. 22. The additives were tested on an existing emulsion sample after four days storage. As shown in FIG. 22, xanthan gum was effective in suppressing sedimentation when used at concentrations of 200 to 500 ppm. Polyethylene glycols of molecular weights 20,000 or 3350 were not effective. Reducing the water content of the emulsion from 30 to 24.5 weight percent was not effective at suppressing sedimentation, although this did increase the bulk viscosity of the emulsion fuel. The effect of xanthan additive concentration is shown in FIG. 23. For treated emulsion samples stored for a short period of time (e.g. one week), sedimentation was suppressed partially by any xanthan concentration from 25 to 200 ppm, with very attractive results at 100 ppm. At or above 200 ppm, the bulk viscosity of the mixed emulsion increased substantially due to the thickening action of the xanthan.

An emulsion was prepared in run BEPU-32 (Batch Emulsion Preparation Unit) with 20 ppm xanthan added along with the water, to test the effect of xanthan on the emulsion preparation process. As shown in Table XXI, a very similar emulsion was prepared with or without xanthan at similar preparation conditions, but the emulsion viscosity with 200 ppm xanthan was 44 percent higher due to bulk thickening action. The long term static stability measurements, as shown in FIG. 24, indicate no benefit of the xanthan in this sample; Xanthan is preferably added to the emulsion after it is prepared and cooled in order to realize the benefit in suppressing sedimentation. Adding xanthan to the emulsion during preparation and/or after preparation but before cooling, does not produce as effective results as adding xanthan after cooling.

The reason for xanthan's ineffectiveness when fed with hot water/surfactant solution is not known for certain. It is believed that thermal stability of the xanthan is responsible: xanthan can lose some of its activity when exposed to elevated emulsion-preparation water could be employed. Preferably, xanthan is metered into the emulsion preparation step from an ambient-temperature day tank.

In a commercial preparation, Xanthan gum may be added to the otherwise finished cooled emulsion quite readily by simply metering a small stream of xanthan in water into the emulsion as it exits the emulsion cooler, and passing the blend through an additional static mixer, or by metering it in upstream of the main mixer. In the latter case the xanthan would be heated for only a few seconds, which would probably be acceptable, compared to a typical four-hour preheat for a BEPU run. The quantity of xanthan used may be tailored to the specific needs of an application, since it is effective over a wide range of concentrations.

In the process of making asphalt fuel emulsions a skim layer of asphalt foam may form on top of the product tank preferably generally comprising less than 1% by wt. of the emulsion. Recycled asphalt "skim" from the emulsion product tank from run PLCEP-111B was emulsified successfully in the Batch Emulsion Prepartion Unit (run BEPU-31B) with the emulsifier of Example XXXXVIII. Preliminary results are very similar to those from a similar run on virgin asphalt feedstock (Run BEPU-19), as shown in Table XXII. Emulsion properties are satisfactory. Therefore it can be concluded that the "skim" material may be reclaimed in a straight-forward manner in a commercial application. A schematic of process provisions for asphalt-skim handling is shown in FIG. 25. The formed asphalt emulsion should be cooled to about 150.degree. F. in the CEP unit. Also, the pressure at the cooler inlet should be maintained at about 20 psig. These design constraints are needed in order to suppress formation of microbubbles in the newly-formed emulsion and thus reduce formation of coagulated droplets of asphalt. The product tank should be equipped to handle small amounts (<0.5%) of asphalt skim and oversize sediment. A surface skimmer should deliver any skim into a receiver which is steam heated to about 250.degree. F. Asphalt skim is dehydrated and intermittently pumped back to the asphalt feed tank by a Moyno-type pump. The product draw should be located somewhat above the tank bottom, to allow a gradual accumulation of asphalt on the bottom. The tank should be heatable with steam to provide for occasional asphalt cleanup. A mixer should be provided to roll the tank intermittently but should not be operated continuously, as this would be detrimental to the asphalt emulsion. The outlet line should be provided with an outlet strainer which can be purged occasionally back to the skim receiver.

The objective of the subject experimental work in this Example was to determine whether an existing asphalt WCE fuel can be reprocessed to remove the oversize portion and/or reduce the average particle size.

The device used to reprocess asphalt WCE fuel was a Gaulin Model 15M-8TA laboratory homogenizer, manufactured by Gaulin Corporation, Garden Street, Everett, Mass. 02149. The emulsion which was reprocessed consisted of off-spec startup/shutdown asphalt emulsion from the CEP unit, screened to exclude any >1500 micron particles and prepared with an asphalt hydrocarbon having a TBP of above about 650.degree. F. and the emulsifying composition of Example XXXXVIII and in accordance with the procedure of Example XXXXVII. As shown in Table XXIII, this emulsion contained about 9 percent >100 micron particles, had d.sub.50 of 23.7 microns, Volumetric mean particle size of 39 microns and dispersity of 4.1. The asphalt emulsion was preheated to about 180.degree. F. The Gaulin emulsifier was preheated to about 170.degree.-180.degree. F. by recirculating surfactant solution under pressure, then draining said solution and replacing it with 2200 cc of preheated asphalt emulsion. The emulsifier was adjusted to a pressure differential of 3000 psi and the emulsion recirculated at a flow rate of 951 g/min. Samples were taken periodically and the particle size distribution measured on an HIAC analyzer. Temperature increased steadily due to power dissipated at the emulsifier valve. As seen in Table XXIII, the average particle size decreased with time and the particle distribution became narrower (lower dispersity). The amount of >100-micron material diminished from 10.1% in the starting material to zero after 20 minutes (8.5 passes through the emulsifier valve).

After 20 minutes' processing at 3000 psi, the pressure differential was increased to 6000 psi. At this increased processing power, the temperature rose relatively quickly and within 4 minutes the emulsion showed substantial coalescence. After 8 minutes the sample had been sheared to the point of phase separation failure. It is believed that the phase separation occurred due to depletion of surfactant content, as may occur during long term emulsion transportation.

A second experiment was performed to test emulsifier performance at 6000 psi differential. At this higher shear intensity the >100-micron material was essentially eliminated more quickly (1.5 vs 5 passes at 3000 psi) but the emulsion moved to essentially the same particle size distribution as was obtained at 3000 psi (compare experiment #2 at 4 minutes with experiment #1 at 20 minutes).

The energy of emulsification is shown in Table XXIII. Minimum particle size, d.sub.50, of 19.3 microns was achieved after 20 minutes at 3000 psi, with energy expenditure of 76 Btu/lb. Minimum particle size, d.sub.50, of 21.1 microns was achieved after 4 minutes at 6000 psi, with energy expenditure of 27 Btu/lb. It would appear that the higher-pressure treatment was more energy efficient in obtaining a similar result. For comparison, the mechanical energy expended initially forming a good asphalt WCE fuel via static mixing is about 0.7 Btu/lb. It is believed, therefore, that reprocessing with a static mixer would also be more energy efficient that use of a pressure disk emulsifier such as the Gaulin.

Recapitulating, experiments using a Gaulin pressure disk emulsifier showed that an off-spec asphalt WCE fuel can be reprocessed back to spec, with removal of oversize particles. Operation of the emulsifier at 6000 psi is more effective and energy efficient than same at 3000 psi, while producing a product of similar particle size distribution. Overshearing of the emulsion can occur shortly after it reaches minimum particle size, resulting in coalescence and phase separation. This is one means of cleanly breaking (demulsifying) an asphalt WCE fuel. Energy requirements for reprocessing by a pressure disk emulsifier greatly exceed those of initially forming a good emulsion via static mixing.

The hydrocarbon was bitumen from the Athabasca tar sands; and the emulsifying composition was water plus NP-9 emulsifying agent additive mixed such that the amount of NP-9 was from about 100 ppm to about 1000 ppm preferably about 200 ppm to about 400 ppm. An OCE was formed by dispersing through agitation (i.e. dynamic and/or static) the water into the hydrocarbon, forming an oil continuous emulsion (OCE) with I0% by wt. water and a water droplet size of mostly 5 to 20 microns. FIG. 26 is a photomicrograph of the oil continuous emulsion having an oil phase OP and a water phase WP1. As clearly shown in FIG. 26, the water phase WP1 comprises a plurality of water phase WP1 droplets (mostly 5 to 20 microns in size) dispersed throughout the oil phase OP. After the OCE of FIG. 26 was prepared, the OCE of FIG. 26 was agitated/blended with an emulsifying composition including water plus a 50/50 mixture of NP40 and NP100 mixed such that the amount of the mixture of NP40 and NP100 was from about 400 ppm to about 2500 ppm (preferably about 700 ppm to 2000 ppm). A water continuous emulsion (as shown in FIG. 27) was produced having a plurality of oil phase OP droplets with a mean oil droplet size of about 50 microns. The oil phase OP droplets are dispersed throughout a water phase WP2. The wt. % of WP1 and WP2 together is from about 25% by wt. to about 35% by wt. of the total weight of the entire double emulsion mixture. As clearly depicted in FIG. 27, water droplet size of the WP1 in the original OCE conforms to a range such that the water droplets are small enough for inclusion within the oil droplets of the oil phase OP of the double emulsion WCE, but large enough to cause explosive secondary atomization. The size of the oil droplets of the oil phase OP in the double emulsion WCE was controlled to an optimum range by the formula d= CD.sup.a N.sub.we.sup.-b. If the oil droplets are too large (e.g. larger than 100 microns or larger), the produced double emulsion WCE lacks stability and would burn poorly. If the oil droplets are too small (e.g. less than about 5 microns), the produced double emulsion becomes excessively viscous and would require too much water to effect atomization.

Repeat Example XXXXXIX but with the OCE being agitated with an emulsifying composition containing the emulsifying agent(s) of Example XXXXVII and find similar results.

Repeat Example XXXXXIX but with the OCE being agitated with an emulsifying composition containing an ethoxylated dialkylphenol compound having the general formula: ##STR49## wherein n.sub.1 is an integer having the value of from about 7 to about 18, and n.sub.2 is an integer having a value of from about 7 to about 18, and y.sub.1 is an integer having a value of from about 4 to about 1000; and said at least one ethoxylated dialkylphenol compound has a molecular weight distribution with a dispersity of from about 1.0 to about 5.0 and with a weight average molecular weight of from about 2519 to about 11,627; and wherein at least about 50% by weight of the emulsifying agent comprises said at least one ethoxylated dialkylphenol compound having a molecular weight of from about 2519 to about 11,627; and from 1% by weight to 90% by weight of the emulsifying agent comprises said at lest one ethoxylated dialkylphenol compound wherein y.sub.1 is greater than 100.

The results are similar to those found in Example XXXXXIX.

Repeat Example XXXXXIX and find a layer of emulsion skim up to about 3% by wt. of the produced double emulsion. The emulsion skim is removed and recycled and admixed with the WCE forming emulsifying composition and/or the OCE to produce a double emulsion WCE.

Repeat Example XXXXXIX and find that the OCE is formed with up to about 3% by wt. skim. This skim is removed and recycled to be admixed with the OCE forming emulsifying composition and/or hydrocarbon (bitumen) and find similar results.

Repeat Example XXXXVII and find that the formed emulsion has a d.sub.50 as being from about 10 to about 20 (preferably about 14 to 16). The formed emulsion is burned with no carbon or fireflies or smoke or soot or other unconverted material or unburned material (i.e. there is an absence of unconverted or unburned material).

While the present invention has been described herein with reference to particular embodiments thereof and examples therefor, a latitude of modification, various changes and substitutions are intended in the foregoing disclosure and it will be appreciated that in some instances some features of the invention will be employed without a corresponding use of other features without departing from the scope of the invention as set forth. For example, while mixing of hydrocarbon crude with the emulsifying composition has been described as taking place above the surface of the earth, it is to be understood that mixing of hydrocarbon crude with the emulsifying composition below the surface of the earth, such as in a tubing of a producing well, is within the spirit and scope of this invention. Similarly, while the production of an oil-in-water emulsion has been described for purposes of transmission through a pipeline, it is to be understood that the spirit and scope of this invention include the production of an oil-in-water emulsion for any suitable purpose including, but not limited to, burning in a burner/boiler, and purposes of transmission through any pipe means. Thus, by way of example only, whenever "pipeline" is referred to in the specification and the claims, it is to be construed to be any pipe means, such as tubing of a producing well.