Polymerization Catalyst, Production and Use

This invention relates to a novel solid catalyst component to be employed with a cocatalyst for use in the polymerization of olefins to polyolefins such as polyethylene, polypropylene and the like, or copolymers such as ethylene copolymers with other alpha-olefins and diolefins, which catalyst component shows unusually high activity, excellent hydrogen response for the contol of polymer molecular weight and good comonomer response for the production of copolymers. The polymer product obtained has a good balance of polymer properties, for example, the catalyst system obtains a polymer with a broad molecular weight distribution and an improved balance in polymer product machine direction tear strength and transverse direction tear strength. As a result, the blown film produced from the polymer product manifests an overall higher strength.

The catalyst component comprises a solid reaction product obtained by contacting a solid, particulate, porous support material such as, for example, silica, alumina, magnesia or mixtures thereof, for example, silica-alumina, with an organoaluminum compound, a vanadium compound and a halogenating agent. The novel catalyst component, which when used with an aluminum alkyl cocatalyst, provides the novel catalyst system of this invention which can be usefully employed for the polymerization of olefins.

The catalyst system can be employed in slurry, single-phase melt, solution and gas-phase polymerization processes and is particularly effective for the production of linear polyethylenes such as high-density polyethylene and linear low denisty polyethylene (LLDPE).

It is known that catalysts of the type generally described as Ziegler-type catalysts are useful for the polymerization of olefins under moderate conditions of temperature and pressure. It is also well known that the properties of polymer product obtained by polymerizing olefins in the presence of Ziegler-type catalysts vary greatly as a function of the monomers of choice, catalyst components, catalyst modifiers and a variety of other conditions which affect the catalytic polymerization process.

For the production of high strength film, it is desirable that polymer product have a high molecular weight. However, high molecular weight resins such as polyethylene, which generally are of a narrow molecular weight distribution are difficult to process.

It is therefore desirable to provide polyolefin resins having a high molecular weight so as to obtain high strength films therefrom coupled with a broad molecular weight distribution so as to provide an easily processable resin. It is furthermore highly desirable that the resin be produced by a commercially feasible and economical process which obtains polymer product having a good balance of properties.

U.S. Pat. No. 4,434,242 of Roling et al, issued Feb. 28, 1984, teaches a polymerization process for preparing injection molded resins by polymerizing ethylene in the presence of a vanadium based catalyst. However, as taught in the patent, the process provides resins having a narrow molecular weight distribution suitable for injection molded resins rather than blown molded resins.

In European Patent Application 55589, Asahi teaches treating an oxide support with an organomagnesium composition, a chlorosilane and then treating with a titanium or vanadium compound that has at least one halogenated atom. As demonstrated in Example 7, the resin obtains a relatively narrow molecular weight distribution which is statistically in the same range as the resins produced in the presence of titanium based catalysts.

British No. 2,105,355 describes a gas-phase method for making elastomeric copolymers of ethylene and higher alpha-olefins in the presence of a vanadium-based catalyst. The catalyst is prepared by sequentially treating an inert oxide support with a vanadium compound, and an aluminum alkyl compound. The catalyst is not taught to be useful for the production of injection molded or blow molded resins but rather produces an elastomeric product.

Soviet 422,192 treats a silica support with an organoaluminum compound and a chlorinating agent and thereafter adds TiCl.sub.4 to the material so as to obtain an active catalyst. The production of polyetylene having a high molecular weight and coupled with a broad molecular weight distribution is not disclosed.

In U.S. Pat. No. 4,435,518 of Pennington a process is disclosed for the production of resins having a narrow molecular weight distribution by polymerizing an olefin in the presence of a catalyst composition comprising an inorganic oxide support treated with an organometallic compound such as trialkylaluminum, further treated with vanadium compound and finally treated with an alcohol.

In U.S. Pat. No. 4,435,519 of Veazey also teaches the production of polyolefins such as polyethylene having a narrow molecular weight distribution in the presence of a vanadium-based catalyst, said catalyst obtained by treating an inorganic oxide support with an organometallic compound such as triethylaluminum, and a vanadium compound.

The above patents do not suggest how its processes might be modified to result in the formation of polymers having a broad molecular weight distribution coupled with a high molecular weight so as to provide resins suitable for the production of high-strength films.

Furthermore, the patents do not disclose catalyst systems which show excellent responsiveness to hydrogen during the polymerization reaction for the control of molecular weight, do not disclose or evidence the excellent comonomer response so as to produce ethylene copolymers and particularly LLDPE, and particularly do not disclose highly active catalyst systems which all produce a high molecular weight-broad molecular weight distributed polymeric resin.

In my cofiled appliction, U.S. Ser. No. 680,871filed Dec. 12, 1984, I disclose a catalyst system comprising a vanadium containing solid obtained by treating an inert support material with an organoaluminum compound, an acid halide and a vanadium compound.

In accordance with this invention catalyst combinations have been found which have extremely high catalytic activites, good comonomer incorporation, excellent hydrogen responsiveness for the control of molecular weight and obtain polymer product manifesting a broad molecular weight distribution with greatly improved film properties. The resins exhibit excellent melt strength with a surprising decrease in power consumption, hence an increase in extrusion rates.

The new catalyst systems and catalyst components of this invention ae obtained by contacting an organoaluminum compound, a halogenating agent and a vanadium metal compound n the presence of an oxide support. The catalyst system employing the vanadium based catalyst component is advantageously employed in a gas phase ethylene polymerization process since there is a significant decrease in reactor fouling as generally compared with prior art ethylene gas phase polymerization processes thereby resulting in less frequent reactor shut downs for cleaning.

In accordance with the objectives of this invention there is provided a vanadium based catalyst component useful for the polymerization of alpha-olefins comprising a solid reaction product obtained by treating an inert solid support material in an inert solvent with (A) an organoaluminum compound, (B) one or more halogenating agents, and, (C) at least one vanadium compound.

The solid vanadium based catalyst component when employed in combination with a cocatalyst such as an alkyl aluminum cocatalyst provides a catalyst system which demonstrates a number of unique properties that are of great importance in the olefin polymerization technology such as, for example, extremely high catalytic activity, the ability to obtain high molecular weight resins and the ability to control the resin molecular weight during the polymerization reaction as a result of the improved responsiveness to hydrogen, increased polymer yield, and reduced reactor fouling. The resin so produced manifests a broad molecular weight distribution coupled with a high molecular weight thereby facilitating the production of films having improved melt strength and tear strength.

In a preferred embodiment of the invention the (A) organoaluminum compound can be represented by the formula R.sub.m AlX.sub.3-m wherein R is a hydrocarbyl radical, X is a halogen atom and m can be greater than 0 to 3, the (B) halogenating agents are chosen from chlorinating, brominating and iodinating agents, and the (C) vanadium compounds are hydrocarbon-soluble vanadium compounds in which the vanadium valence is 3 to 5. Mixtures of the vanadium compounds can be employed. The halogenating agents can be selected from weak or strong halogenating agents and are suitably employed in order to obtain the broadest molecular weight distribution. Use of the weak halogenating agents results in a resin product having a broader molecular weight distribution as compared with that obtained when using a strong halogenating agent. Nevertheless, the strong halogenating agents obtain resins having broader molecular weight distribution than those obtained in the absence of halogenating agents. Furthermore, the strong halogenating agents greatly enhance catalytic activity.

Although, in accordance with this invention, the order of addition in ingredients in forming the vanadium containing catalyst component can vary, the catalyst component is preferably prepared by either reacting the (A) organoaluminum compound with the inert solid support material which is preferably a Group IIa, IIIa, IVa or IVb metal oxide, or a finely divided polyolefin or other suitable support material and thereafter subjecting the system to treatment with the halogen containing compound followed by treatment with the vanadium compound or in the alternative reacting the (C) vanadium compound with the support and thereafter subjecting the system to treatment with the vanadium compound and finally the halogen containing compound.

In a second embodiment of this invention there is provided a catalyst system comprising the vanadium containing solid catalyst component and an organoaluminum cocatalyst for the polymerization of alpha-olefins using the catalyst of this invention under conditions characteristic of Ziegler polymerization.

In view of the high activity of the catalyst system prepared in accordance with this invention as compared with conventional vanadium based catalysts, it is generally not necesary to deash polymer product since polymer product will generally contain lower amounts of catalyst residues than polymer product produced in the presence of conventional catalyst.

The catalyst systems can be employed in a gas phase process, single phase melt process, solvent process or slurry process. The catalyst system is usefully employed in the polymerization of ethylene and other alpha-olefins, particularly alpha-olefins having from 3 to 8 carbon atoms and copolymerization of these with other 1-olefins or diolefins having from 2 to 20 carbon atoms, such as propylene, butene, pentene and hexene, butadiene, 1,4-pentadiene and the like so as to form copolymers of low and medium densities. The supported catalyst system is particularly useful for the polymerization of ethylene and copolymerization of ethylene with other alpa-olefins in gas phase processes to produce LLDPE or HDPE.

Briefly, the catalyst components of the present invention comprise the treated solid reaction product of (A) an organoaluminum compound, (B) a halogenating agent, and (C) a vanadium compound in the presence of an inert support material. According to the polymerization process of this invention, ethylene, at least one alpha-olefin having 3 or more carbon atoms or ethylene and other olefins or diolefins having terminal unsaturation are contacted with the catalyst under polymerizing conditions to form a commercially useful polymeric product. Typically, the support can be any of the solid particulate porous supports such as talc, silica, zirconia, thoria, magnesia, an titania. Preferably the support material is a Group IIa, IIIa, IVa and IVb metal oxide in finely divided form.

Suitable inorganic oxide materials which are desirably employed in accordance with this invention include silica, alumina, and silica-alumina and mixtures thereof. Other inorganic oxides that may be employed either alone or in combination with the silica, alumina or silica-alumina are magnesia, titania, zirconia, and the like. Other suitable support materials, however, can be employed. For example, finely divided polyolefins such as finely divided polyethylene.

The metal oxides generally contain acidic surface hydroxyl groups which will react with the organometallic composition or transition metal compound first added to the reaction solvent. Prior to use, the inorganic oxide support is dehydrated, i.e., subject to a thermal treatment in order to remove water and reduce the concentration of the surface hydroxyl groups. The treatment is carried out in vacuum or while purging with a dry inert gas such as nitrogen at a temperature of about 100.degree. to about 1000.degree. C., and preferably from about 300.degree. C. to about 800.degree. C. Pressure considerations are not critical. The duration of the thermal treatment can be from about 1 to about 24 hours. However, shorter or longer times can be employed provided equilibrium is established with the surface hydroxyl groups.

Chemical dehydration as an alternative method of dehydration of the metal oxide support material can advantageously be employed. Chemical dehydration converts all water and hydroxyl groups on the oxide surface to inert species. Useful chemical agents are, for example, SiCl.sub.4, chlorosilanes, silylamines and the like. The chemical dehydration is accomplished by slurrying the inorganic particulate material in an inert hydrocarbon solvent, such as, for example, heptane. During the dehydration reaction, the silica should be maintained in a moisture and oxygen-free atmosphere. To the silica slurry is then added a low boiling inert hydrocarbon solution of the chemical dehydrating agent, such as, for example, dichlorodimethylsilane. The solution is added slowly to the slurry. The temperature range during the chemical dehydration reaction can be from about 25.degree. C. to about 120.degree. C., however, higher and lower temperatures can be employed. Preferably the temperature will be from about 50.degree. C. to about 70.degree. C. The chemical dehydration procedure should be allowed to proceed until all the moisture is removed from the particulate support material, as indicated by cessation of gas evolution. Normally, the chemical dehydration reaction will be allowed to proceed from about 30 minutes to about 16 hours, preferably 1 to 5 hours. Upon completion of the chemical dehydration, the solid particulate material is filtered under a nitrogen atmosphere and washed one or more times with a dry, oxygen-free inert hydrocarbon solvent. The wash solvents, as well as the diluents employed to form the slurry and the solution of chemical dehydrating agent, can be any suitable inert hydrocarbon. Illustrative of such hydrocarbons are heptane, hexane, toluene, isopentane and the like.

The preferred (A) organoaluminum compounds employed in this invention can be represented by the general formula R.sub.m AlX.sub.3-n wherein R represents an alkyl group, cycloalkyl group or aryl group, X represents a halogen atom and m represents a suitable numeral within the range of 1.ltoreq.m.ltoreq.3, or mixtures or complex compounds thereof. In particular, it is preferable to employ alkyl aluminum compounds wherein the alkyl groups have from 1 to 18 carbon atoms, preferably 1 to 9 carbon atoms. Illustrative but non-limiting examples of the organoaluminum compounds which may be suitably employed are the trialkylaluminums such as trimethyl aluminum, triethyl aluminum, tributyl aluminum, triisobutyl aluminum, tri-n-pentyl aluminum, tri-n-octyl aluminum, and the like. Illustrative examples of the dialkyl aluminum halides are diethyl aluminum chloride, diethyl aluminum fluoride, dimethyl aluminum chloride, dibutyl aluminum chloride, diethyl aluminum bromide, diethyl aluminum iodide and dibutyl aluminum iodide. Examples of the monoalkyl aluminum dihalides are methyl aluminum dichloride, ethyl aluminum dichloride, butyl aluminum dichloride, isobutyl aluminum dichloride, ethyl aluminum dibromide, ethyl aluminum diiodide, butyl aluminum dibromide and butyl aluminum diiodide. Moreover, the sesquihalides can be suitably employed such as ethyl aluminum sesquichloride and the like.

The molecular weight distribution is affected by the aluminum alkyls of choice. For example, the aluminum alkyls comprising the more reactive alkyl groups when employed result in a broader molecular weight distribution resin as reflected in the melt index ratio values as compared with those resins produced from the less reactive aluminum alkyls. It is also found that the catalyst prepared from the halide containing aluminum alkyls resulted in obtaining resins of broader molecular weight distribution. The preferred aluminum alkyls to be employed in accordance with this invention, therefore, are trimethyl aluminum, diethyl aluminum fluoride, isobutyl aluminum dichloride and ethyl aluminum dichloride.

The aluminum alkyls can be conveniently added to the agitated slurry containing the inert particulate support such as silica in liquid form, i.e., the aluminum alkyl is in solution, e.g., in hexane, benzene, toluene, etc. Alternatively, the aluminum alkyl can be added to the slurry in undiluted form.

In accordance with this invention, the halogenating agents are employed to obtain increased catalytic activity over similar catalyst systems absent the halogenating agent. It has been discovered that the use of halogenating agents in order to obtain the desirable increase in activity is accomplished without detrimentally affecting the broad molecular weight distribution obtained in accordance with this invention. The halogenating agents which can be employed are chlorinating, brominating and iodinating agents. The halogenating agents are desirably strong halogenating agents, nevertheless, the use of weaker halogenating agents which results in the production of resins with the broadest molecular weight distribution are desirable. The halogenating agents can be liquid or gaseous under the reaction conditions.

Illustrative but non-limiting examples of the strong halogenating agents that can be usefully employed in accordance with this invention are the silicon halides and the hydrocarbyl halides.

The silicon halides can be represented by the formula X.sub.m SiR.sub.n in which X is a halogen, R is an alkyl, cycloalkyl or aryl radical containing 1 to 20 carbon atoms, n+m=4 and m is at least 1. Illustrative examples of the silicon compounds are silicon tetrachloride, silicon tetrabromide, chlorosilanes such as, for example, trimethylchlorosilane, dimethyldichlorosilane, ethyltrichlorosilane, diethyldichlorosilane, dichlorodibutylsilane, trichlorobutylsilane, tribromobutylsilane, bromotrimethylsilane, and the like.

The hydrocarbyl halides include carbon tetrachloride, chloroform, 1,1,1-trichloroethane, dichloromethane, trichlorofluoromethane and the like.

The preferred chlorinating agents are strong activating chlorinating agents amongst which the most preferred are silicon tetrachloride trichlorofluoromethane, trichloroethane and the like.

Illustrative of the weak activating chlorinating agents are the thionyl halides such as SOCl.sub.2.

The halogen-containing compound is conveniently added to the reaction slurry which comprises the solid particulate material, or the solid reaction product from the treatment of the solid particulate material and the aluminum alkyl. The addition of the halogen containing compound can be effected by using a solution of the halogen-containing compound in an inert solvent such as, for example, a aliphatic hydrocarbon solvent or a aromatic hydrocarbon solvent. The halogen-containing compound can also be added as a gas. The halogen-containing compound can also be added at two separate steps during the catalyst component preparation, for example, after the aluminum alkyl treatment and thereafter after the vanadium compound treatment.

The vanadium compound which can be usefully employed in the preparation of the vanadium containing catalyst component of this invention are well known in the art and can be represented by the formulas ##STR1## where x=0-3 and R=a hydrocarbon radical:

where y=3-4 and R=a hydrocarbon radical; ##STR2## where z=2-3 and (AcAc)=acetyl acetonate group; ##STR3## where (AcAc)=acetyl acetonate group; and

where n=2-3 and B=Lewis base, such as tetrahydrofuran, which can form hydrocarbon-soluble complexes with VCl.sub.3.

In formulas 1 and 2 above, R preferably represents a C.sub.1 to C.sub.8 aliphatic radical free of aliphatic unsaturation or aromatic hydrocarbon radicl such as straight- or branded-chemical alkyl, aryl, cycloalkyl, alkanyl, aralkyl group such as methyl, ethyl, propyl, isopropyl, butyl, n-butyl, i-butyl, t-butyl, pentyl, hexyl, cyclohexyl, octyl, benzyl, dimethyl, phenyl, naphthyl, etc.

Illustrative, but non-limiting examples of the vanadium compounds are vanadyl trichloride, vanadium tetrachloride, vanadium tetrabutoxy, vanadium trichloride, vanadyl acetylacetonate, vanadium acetylacetonate, vanadyl dichloroacetylacetonate, vanadyl chloradiacetylacetonate, vanadium trichloride complexed with tetrahydrofuran, vanadyl tribromide, vanadium tetrabromide, and the like.

The vanadium compound is preferably added to the reaction mixture in the form of a solution. The solvent can be any of the well-known inert hydrocarbon solvents such as hexane, heptane, benzene, toluene, and the like.

The treatment of the support material as mentioned above is conducted in an inert solvent. The inert solvent can be the same as that employed to dissolve the individual ingredients prior to the treatment step. Preferred solvents include mineral oils and the various hydrocarbons which are liquid at reaction temperatures and in which the individual ingredients are soluble. Illustrative examples of useful solvents in addition to those mentioned above include the alkanes such as pentane, iso-pentane, hexane, heptane, octane and nonane; cycloalkanes such as cyclopentane, cyclohexane; and aromatics such as benzene, toluene, ethylbenzene and diethylbenzene. The amount of solvent employed is not critical. Nevertheless, the amount employed should be sufficient so as to provide adequate heat transfer away from the catalyst components during reaction and to permit good mixing.

The amounts of catalytic ingredients employed in the preparation of the solid catalyst component can vary over a wide range. The concentration of aluminum alkyl deposited on the essentially dry, inert support can be in the range from about 0.1 to about 3 millimoles/g of support, however, greater or lesser amounts can be usefully employed. Preferably, the organoaluminum compound concentration is in the range of 0.1 to 2.0 millimoles/g of support and more preferably in the range of 0.4 to 0.8 millimoles/g of support. The amount of halogenating agent employed should be such as to provide a halogen to aluminum mole ratio of about 1 to about 100 and preferably 4 to 40.

The vanadium compound is added to the inert support reaction slurry at a concentration of about 2.0 to about 0.05 millimoles V/g of dried support, preferably in the range of about 1.4 to about 0.14 millimoles V/g of dried support and especially in the range of about 0.2 to 0.6 millimoles V/g of dried support. The support is dried at a temperature between 300.degree. and 800.degree. C. using methods well known to those skilled in the art.

Generally, the individual reaction steps can be conducted at temperatures in the range of about -50.degree. C. to about 150.degree. C. Preferred temperature ranges are from about -30.degree. C. to about 60.degree. C. with -10.degree. C. to about 50.degree. C. being most preferred. The reaction time for the individual treatment steps can range from about 5 minutes to about 24 hours. Preferably the reaction time will be from about 1/2 hour to about 8 hours. During the reaction constant agitation is desirable.

In the preparation of the vanadium metal-containing solid catalyst component, washing after the completion of any step may be effected.

The catalyst components prepared in accordance with this invention are usefully employed with cocatalysts well known in the art of the Ziegler catalysis for polymerization of olefins. Typically, the cocatalysts which are used together with the transition metal containing catalyst component are organometallic compounds of Group Ia, IIa and IIIa metals such as aluminum alkyls, aluminum alkyl hydrides, lithium aluminum alkyls, zinc alkyls, magnesium alkyls and the like. The cocatalysts preferably used are the organoaluminum compounds. The preferred alkylaluminum compounds are represented by the formula AIR'.sub.n X'.sub.3-n wherein R' is hydrogen, hydrocarbyl or substituted hydrocarbyl group and n is as defined herein above. Preferably R' is an alkyl group having from 2 to 10 carbon atoms. Illustrative examples of the cocatalyst material are ethyl aluminum dichloride, ethyl aluminum sesquichloride, diethyl aluminum chloride, aluminum triethyl, aluminum tributyl, diisobutyl aluminum hydride, diethyl aluminum ethoxide and the like. Aluminum trialkyl compounds are most preferred with triisobutylaluminum and aluminum triethyl being highly desirable. X' is halogen and preferably chlorine.

The catalyst system comprising the aluminum alkyl cocatalyst and the vanadium metal containing solid catalyst component is usefully employed for the polymerization of ethylene, other alpha-olefins having from 3 to 20 carbon atoms, such as for example, propylene, butene-1, pentene-1, hexene-1, 4-methylpentene-1, and the like and ethylene copolymers with other alpha-olefins or diolefins such as 1,4-pentadiene, 1,5-hexadiene, butadiene, 2-methyl-1,3-butadiene and the like. The polymerizable monomer of preference is ethylene. The catalyst system may be usefully employed to produce polyethylene or copolymers or ethylene by copolymerizing with other alpha-olefins or diolefins, particularly propylene, butene-1, pentene-1, hexene-1, and octene-1. The catalyst is especially useful for the preparation of high molecular weight LLDPE and HDPE and have broad molecular weight distribution. Typically the polymers will have melt indexes from 0.01-1.0 and MIR from about 100 to about 200. The olefins can be polymerized in the presence of the catalysts of this invention by any suitable known process such as, for example, suspension, solution and gas-phase processes.

The polymerization reaction employing catalytic amounts of the above-mentioned solid catalyst can be carried out under conditions well known in the art of Ziegler polymerization, for example, in an inert diluent at a temperature in the range of 50.degree. C. to 120.degree. C. and a pressure of 1 to 40 atmospheres in the gas phase at a temperature range of 70.degree. C. to 100.degree. C. at about 1 atmosphere to 50 atmospheres and upward. Illustrative of the gas-phase processes are those disclosed in U.S. Pat. No. 4,302,565 and U.S. Pat. No. 4,302,566, which references are hereby incorporated in their entirety by reference. As indicated above, one advantageous property of the catalyst system of this invention is the reduced amount of gas phase reactor fouling. The catalyst system can also be used to polymerize olefins at single phase conditions, i.e., 150.degree. C. to 320.degree. C. and 1,000-3,000 atmospheres. At these conditions the catalyst lifetime is short but the activity sufficiently high that removal of catalyst residues from the polymer is unnecessary. However, it is preferred that the polymerization be done at pressures ranging from 1 to 50 atmospheres, preferably 5 to 25 atmospheres.

Improved yields can be further obtained by employing polymerization promoters (activators) in combination with the catalyst system of this invention. The polymerization activators, in accordance with this invention, are preferably chlorocarbon activators. The activators are generally added to the polymerization reactor as a separate component. However, in the alternative, the activator can be adsorbed onto the surface of the catalyst component of this invention. The activator serves to significantly increase the productivity of the catalyst. Illustrative but non-limiting examples of the chlorocarbons are CHCl.sub.3, CFCl.sub.3, CH.sub.2 Cl.sub.2, ethyltrichloroacetate, methyltrichloroacetate, hexachloropropylene, butylperchlorocrotonate, 1,3-dichloropropane, 1,2,3-trichloropropane, and 1,1,2-trichlorotrifluoroethane, etc. The activators may be gases or liquids at the conditions of polymerization.

In the processes according to this invention it has been discovered that the catalyst system is highly responsive to hydrogen for the control of molcular weight. Other well known molecular weight controlling agents and modifying agents, however, may be usefully employed.

The polyolefins prepared in accordance with this invention can be extruded, mechanically melted, cast or molded as desired. They can be used for plates, sheets, films and a variety of other objects.

While the invention is described in connection with the specific examples below, it is understood that these are only for illustrative purposes. Many alternatives, modifications and variations will be apparent to those skilled in the art in light of the below examples and such alternatives, modifications and variations fall within the general scope of the claims.

In the Examples following the silica support was prepared by placing Davison Chemical Company G-952 silica gel in a vertical column and fluidizing with an upward flow of N.sub.2. The column was heated slowly to between 400.degree. and 800.degree. C. and held at that temperature for 12 hours after which the silica was cooled to ambient temperature.

The melt index (MI) and melt index ratio (MIR) were measured in accordance with ASTM test D1238.

Silica gel (4.0 g Davison 952, dehydrated at 400.degree. C.) was charged to a 125 ml vial and slurried in 25 ml of degassed and dried hexane. To the stirred slurry there was then charged 5.2 moles of trimethyl aluminum in 3.7 ml of heptane solution. The reaction slurry was maintained at ambient temperatures for 1 hour. To the slurry was then added 52 mmoles of neat silicon tetrachloride and the reaction slurry was again maintained at ambient temperatures for 1 hour. Finally, 0.24 mmoles of vanadyl chloride in 0.7 ml of hexane solution was dropwise added to the slurry at ambient temperatures with constant stirring. The reaction mixture was maintained at ambient temperatures for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.5 liter autoclave was charged 800 ml of purified hexane, 0.9 mmoles of triisobutylaluminum in 1.0 ml of heptane slution and 0.30 g of the vanadium containing catalyst component prepared above in 6.4 ml of white oil. The temperature of the reactant was raised to 85.degree., pressured to 30 psig of H.sub.2 and finally pressured to 300 psig with ethylene. The pressure was maintained by constant flow of ethylene. Polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure, cooled, and the polymer slurry filtered. The resulting polymer had an MI of 0.07 and an MIR of 190.6. The specific activity (Kgr PE/g-V-hr-atm) was 15.9.

Catalyst formulations were prepared in a similar manner to Example 1 with the exception that different chlorinating agents and/or aluminum alkyls were employed in the preparation. Detals of the ingredients are summarized in Table 1. The results of the polymerization with respect to MI, MIR and specific activity are also summarized in Table 1.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml heptane. To the vial was added 1.2 mmoles of trimethylaluminum in 0.89 ml of hexane solution to provide an aluminum alkyl to --OH present in the silica surface of 0.5. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 1.2 mmoles of neat silicon tetrachloride to provide a ratio of 1 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour at 32.degree. C. To the vial at room temperature there was added dropwise and with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane solution. The reaction mixture was maintained at 32.degree. C. for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.64 mmoles triisobutyl aluminum in 3 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of the vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 10 psig with hydrogen, and pressured to a total pressure of 150 psig with ethylene. The polymerization was maintained for 40 minutes. The butene-1 to ethylene-1 ratio of 0.587 was maintained by constant ethylene flow and butene-1 injection. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.62, a MIR of 114.4 and the catalyst had a specific activity of 99.4 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 13 the catalyst was prepared identically as in Example 12 with the exception that trichlorofluoromethane was substituted for the silicon tetrachloride, isobutyl aluminum dichloride was substituted for trimethylaluminum and the ratio of aluminum alkyl to silica --OH groups was increased to 1. The results of the polymerization are summarized in Table 2.

In Example 14 the catalyst component was prepared identically as in Example 12 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, tri-n-octyl aluminum was substituted for trimethyl aluminum in an amount so as to provide an aluminum alkyl to --OH ratio in the silica of 1.5. Polymerization was performed unders conditions identical to Example 12. The results of the polymerization are summarized in Table 2.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 2.5 mmoles of diethylaluminumfluoride in 1.4 ml of hexane solution to provide an aluminum alkyl to --OH present in the silica surface of 1.0. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 7.5 mmoles of silicon tetrachloride in 0.86 ml of hexane solution to provide a ratio of 3 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour at 32.degree. C. To the vial at room temperature there was added dropwise with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane solution. The reaction mixture was maintained at 32.degree. C. for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 moles triisobutyl aluminum in 3 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 10 psig with hydrogen, 30 cc of 1-butene and pressured to a total pressure of 150 psig with ethylene. The polymerization was maintained for 40 minutes. The butene-1 to ethylene-1 ratio of 0.587 was maintained by constant ethylene flow and butene-1 injection. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 1.12, a MIR of 127.7 and a specific activity of 82.6 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 16 the catalyst was prepared identically as in Example 15 with the exception that CFCl.sub.3 was substituted for the silicon tetrachloride, tri-n-octyl aluminum was substituted for diethylaluminum fluoride in the amount so as to provide aluminum alkyl to --OH ratio of 0.5. The results of the polymerization are summarized in Table 2.

In Example 17 the catalyst was prepared identically as in Example 15 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, isobutylaluminum dichloride was substituted for diethylaluminum fluoride in the amount so as to provide aluminum alkyl to --OH ratio of 2.0. The results of the polymerization are summarized in Table 2.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 4.1 mmoles of isobutylaluminum dichloride in 3.4 ml of hexane solution to provide an aluminum alkyl to --OH present in the silica surface of about 1.5. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 26 mmoles of neat silicon tetrachloride to provide a ratio of 6.3 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour at 32.degree. C. To the vial at 32.degree. C. there was added dropwise and with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane solution. The reaction mixture was maintained at 32.degree. C. for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3 ml of hexane. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 10 psig with hydrogen, 30 cc of 1-butene and pressured to a total pressure of 150 psig with ethylene. The polymerization was maintained for 40 minutes. The butene-1 to ethylene-1 ratio of 0.587 was maintained by constant ethylene flow and butene-1 injection. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.89, a MIR of 126.0 and a specific activity of 180.6 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 19 the catalyst was prepared identically as in Example 18 with the exception that trichlorofluoromethane was substituted for the SiCl.sub.4, trimethylaluminum for isobutylaluminum dichloride in the amount so as to provide aluminum alkyl to --OH ratio of 2. The results of the polymerization are summarized in Table 2.

In Example 20 the catalyst was prepared identically as in Example 18 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, diethylaluminum fluoride was substituted for isobutyl aluminum dichloride and the aluminum alkyl to --OH ratio was increased to 2. The results of the polymerization are summarized in Table 2.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 5.0 mmoles of tri-n-octylaluminum in 10.7 ml of hexane to provide an aluminum alkyl to --OH present in the silica surface of 2.0. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 50 mmoles of neat silicon tetrachloride to provide a ratio of 10 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour at 32.degree. C. To the vial at 32.degree. C. there was added dropwise and with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane. The reaction mixture was maintained at 32.degree. C. for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3.0 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 10 psig with hydrogen, 30 cc of 1-butene and pressured to a total pressure of 150 psig with ethylene. The polymerization was maintained for 40 minutes. The butene-1 to ethylene-1 ratio of 0.587 was maintained by constant ethylene flow and butene-1 injection. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.62, a MIR of 114.4 and a specific activity of 99.4 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 22 the catalyst was prepared identically as in Example 21 with the exception that trichlorofluoromethane was substituted for the silicon tetrachloride, diethyl aluminum fluoride was substituted for tri-n-octylaluminum and the aluminum alkyl to --OH ratio was increased to 1. The results of the polymerization are summarized in Table 2.

In Example 23 the catalyst was prepared identically as in Example 21 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, trimethylaluminum was substituted for tri-n-octylaluminum and the aluminum alkyl to --OH ratio was increased to 1. The results of the polymerization are summarized in Table 2.

The catalyst was prepared as described in Example 12.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3.0 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 20 psig with hydrogen and pressured to a total pressure of 150 psig which was maintained by constant ethylene flow. The polymerization was maintained for 40 minutes. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 1.04, a MIR of 147.1 and a specific activity of 90.0 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 25 the catalyst was prepared identically as in Example 24 with the exception that trichlorofluoromethane was substituted for the silicon tetrachloride, isobutyl aluminum dichloride was substituted for trimethylaluminum and the aluminum alkyl to --OH ratio was increased to 1. The results of the polymerization are summarized in Table 3.

In Example 26 the catalyst component was prepared identically as in Example 24 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, tri-n-octyl aluminum was substituted for trimethyl aluminum in an amount so as to provide an aluminum alkyl to --OH ratio in the silica of 1.5. Polymerization was performed under conditions identical to Example 24. The results of the polymerization are summarized in Table 3.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 2.4 mmoles of diethylaluminum fluoride in 1.4 ml of hexane to provide an aluminum alkyl to --OH present in the silica surface of 1.0. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 7.5 mmoles of neat silicon tetrachloride to provide a ratio of 3 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour 32.degree. C. To the vial at 32.degree. C. there was added dropwise and with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane solution. The reaction mixture was maintained at ambient temperatures for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3 ml of hexane. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 20 psig with hydrogen and pressured to a total pressure of 150 psig which was maintained by constant ethylene flow. The polymerization was maintained for 40 minutes. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.30, a MIR of 123.4 and a specific activity of 67.5 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 28 the catalyst was prepared identically as in Example 27 with the exception that trichlorofluoromethane was substituted for the silicon tetrachloride, tri-n-octylaluminum was substituted for trimethylaluminum and the aluminum alkyl to --OH ratio was increased to 0.5. The results of the polymerization are summerized in Table 3.

In Example 29 the catalyst component was prepared identically as in Example 27 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, isobutylaluminum dichloride was substituted for trimethyl aluminum in an amount so as to provide an aluminum alkyl to --OH ratio in the silica of 2.0. Polymerization was performed under conditions identical to Example 27. The results of the polymerization are summarized in Table 3.

The catalyst was prepared identically as in Example 18.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 30 psig with hydrogen, 30 cc of 1-butene and pressured to a total pressure of 150 psig which was maintained by constant ethylene flow. The polymerization was maintained for 40 minutes. The butene-1 to ethylene-1 ratio of 0.587 was maintained by constant ethylene flow and butene-1 injection. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.69, a MIR of 128.0 and a specific activity of 107.5 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 31 the catalyst was prepared identically as in Example 30 with the exception that trichlorofluoromethane was substituted for the silicon tetrachloride, trimethylaluminum was substituted for isobutylaluminum dichloride and the aluminum alkyl to --OH ratio was increased to 2.0. The results of the polymerization are summarized in Table 3.

In Example 32 the catalyst component was prepared identically as in Example 30 with the exception that 1,1,1-trichlorethane was substituted for the silicon tetrachloride, diethylaluminum fluoride was substituted for isobutylaluminum dichloride in an amount so as to provide an aluminum alkyl to --OH ratio in the silica of 0.5. Polymerization was performed under conditions identical to Example 30. The results of the polymerization are summarized in Table 3.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C.) was charged to a 125 ml vial and slurried in 20 ml heptane solution. To the vial was added 5.0 mmoles of tri-n-octylaluminum in 10.7 ml of hexane solution to provide an aluminum alkyl to --OH present in the silica surface of 2.0. The reaction slurry was stirred for 1 hour at 32.degree. C. To the reaction slurry was added 50 mmoles of neat silicon tetrachloride to provide a ratio of 10 mmole silicon tetrachloride per mole of aluminum alkyl. The reaction mixture was stirred for 1 hour at 32.degree. C. To the vial at room temperature there was added dropwise and with constant stirring 0.98 mmoles of vanadyl trichloride in 2.8 ml of hexane solution. The reaction mixture was maintained at ambient temperatures for 1 hour. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave was charged 800 ml of purified dry hexane followed by 2.6 mmoles triisobutyl aluminum in 3.0 ml of hexane solution. Freon-11 activator was then injected into the reactor to obtain a 200:1 molar ratio of activator to vanadium containing catalyst component. A white oil slurry containing 0.25 g of vanadium containing catalyst (0.5 gm/cc) was injected into the reactor via a syringe. The reactor was heated to 85.degree. C., pressured to 30 psig with hydrogen and pressured to a total pressure of 150 psig which was maintained by constant ethylene flow. The polymerization was maintained for 40 minutes. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 5.7, a MIR of 55.4 and a specific activity of 98.8 Kg PE/gV-hr-m/1C.sub.2.sup.=.

In Example 34 the catalyst was prepared identically as in Example 33 with the exception that triechlorofluoromethane was substituted for the silicon tetrachloride, diethylaluminum fluoride was substituted for tri-n-octylaluminum and the aluminum alkyl to --OH ratio was increased to 1.5. The results of the polymerization are summarized in Table 3.

In Example 35 the catalyst component was prepared identically as in Example 33 with the exception that 1,1,1-trichloroethane was substituted for the silicon tetrachloride, trimethylaluminum was substituted for tri-n-octylaluminum in an amount so as to provide an aluminum alkyl to --OH ratio in the silica of 1.0. Polymerization was performed under conditions identical to Example 33. The results of the polymerization are summerized in Table 3.

Silica gel (5.0 g, Davison 952, dehydrated at 500.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 1.6 ml of a 0.7 mmol/ml solution of Vanadium oxytrichloride in hexane. The reaction slurry was stirred for 1 hour at 40.degree. C. The supernatant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 2.5 ml of a 1.2 mmol/ml solution of Isobutylaluminum Dichloride in heptane for a total 3.0 mm Isobutylaluminum Dichloride. The reaction slurry was stirred for 1 hour at 23.degree. C. To the vial was then added 1.0 ml (8.7 mmoles) of neat silicon tetrachloride. The reaction mixture was stirred for 1 hour at 23.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 3.6 mm triisobutyl aluminum in 4 ml of hexane solution. A white oil slurry containing 0.26 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 44 mm H.sub.2 was added, 320 mmoles of butene were added, then pressured to a total of 150 psig with ethylene. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure, and the polymer recovered and dried. The polymer had a MI of 0.05, a MIR of 160. The catalyst had a specific activity of 65.5 Kg/PE/gV.mole.1.sup.-1.atm, and a productivity of 200 g PE/g catalyst.

Silica gel (5.0 g, Davison 952, dehydrated at 500.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 1.6 ml of a 0.7 mmol/ml solution of Vanadium oxytrichloride in hexane. The reaction slurry was stirred for 1 hour at 40.degree. C. The supernatant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 2.5 ml of a 1.2 mmol/ml solution of Isobutylaluminum Dichloride in heptane for a total 3.0 mm Isobutylaluminum Dichloride. The reaction slurry was stirred for 1 hour at 23.degree. C. To the vial was then added 2.0 ml of neat silicon tetrachloride for a total of 17.4 mmoles. The reaction mixture was stirred for 1 hour at 23.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 3.6 mm triisobutyl aluminum in 4 ml of hexane solution. A white oil slurry containing 0.25 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 44 mm H.sub.2 was added, 0.320 moles butene was added, then pressured to a total of 150 psig with ethylene. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.06, a MIR of 116.6 and a density of 0.9437 g/cc. The catalyst had a productivity of 188 g PE/g catalyst.

Silica gel (5.0 g, Davison 952, dehydrated at 500.degree. C.) was charged to a 125 vial and slurried in 20 ml hexane. To the vial was added 4.0 ml of a 0.7 mmol/ml solution of vanadium oxytrichloride in hexane to provide an --OH to vanadium ratio of 2.4. The reaction slurry was stirred for 1 hour at 40.degree. C. The supernatant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 2.5 ml of a 1.2 mmol/ml solution by isobutylaluminum dichloride in heptane for a total 3.0 mm isobutylaluminum dichloride. This provided an aluminum alkyl to --OH ratio of 0.41. The reaction slurry was stirred for 1 hour at 23.degree. C. To the vial was then added 1.0 ml of neat silicon tetrachloride for a total of 8.7 mmoles. This provided a chlorine to aluminum alkyl ratio of 3.2. The reaction mixture was stirred for 1 hour at 23.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 1.8 mm triisobutyl aluminum in 2 ml of hexane solution. A white oil slurry containing 0.125 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 44 mm H.sub.2 was added, 320 mmoles of butene were added, then pressured to a total of 150 psig with ethylene. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure, and the polymer recovered and dried. The polymer had a MI of 0.05, a MIR of 165.8 and a specific activity of 111.8 and a productivity of 896.

Silica gel (5.0 g, Davison 952, dehydrated at 800.degree. C. dehydrated in pilot plant 9787-24-6) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 2.8 ml of a 0.7 mmol/ml solution of vanadium oxytrichloride in hexane. The reaction slurry was stirred for 1 hour at 40.degree. C. The supernatant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 3.4 ml of a 1.2 mmol/ml solution of isobutylaluminum dichloride in heptane for a total 4.1 mm isobutylaluminum dichloride. The reaction slurry was stirred for 1 hour at 40.degree. C. To the vial was then added 0.5 ml of an 8.7 mmol/ml solution of silicon tetrachloride for a total of 4.4 mm. The reaction mixture was stirred for 1 hour 40.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 1.8 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 3.6 mm triisobutyl aluminum in 4 ml of hexane solution. A white oil slurry containing 0.25 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 88 mm H.sub.2 was added, and the reactor was pressured to a total of 150 psig with ethylene. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The polymer had a MI of 0.10, a MIR of 171 and a density of 0.9597 g/ cc. The catalyst had a productivity of 522 g PE/g catalyst. Resin density 0.9597.

Silica gel (5.0 g, Davison 952, dehydrated at 500.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 5.0 ml of a 0.7 mmol/ml solution of vanadium oxytrichloride in hexane. The reaction slurry was stirred for 1 hour at 40.degree. C. The superntant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 3.1 ml of a 1.2 mm molar ml solution of isobutylaluminum dichloride in heptane for a total 3.72 mm isobutylaluminum dichloride. The reaction slurry was stirred for 1 hour at 23.degree. C. To the vial was then added 1.6 ml of neat solution of silicon tetrachloride giving a total of 13.9 mm. The reaction mixture was stirred for 1 hour at 23.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 2.1 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 1.8 mm triisobutyl aluminum in 2 ml of hexane solution. A white oil slurry containing 0.125 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 65 mm H.sub.2 was added, 175 ml hexene was added, then pressured to a total of 150 psig with ethylene. The polymerization was maintained for 46 minutes at which time the reactor was vented to atmospheric pressure and the polymer recovered and dried. The catalyst exhibited a specific activity of 39.6 Kg Pe/gV.mole.1.sup.-1.atm and a productivity of 304. The resin had a density of 0.9503 g/cc.

Silica gel (5.0 g, Davison, 952, dehydrated at 500.degree. C.) was charged to a 125 ml vial and slurried in 20 ml hexane. To the vial was added 3.0 ml of a 0.7 mmol/ml solution of vanadium oxytrichloride in hexane. The reaction slurry was stirred for 1 hour at 40.degree. C. The supernatant was decanted and the catalyst washed with hexane. The wash was decanted and 20 ml of fresh hexane was added to the vial. To the reaction slurry was added 3.1 ml of a 1.2 mmol/ml solution of isobutylaluminum dichloride in heptane for a total 3.7 mm isobutylaluminum dichloride. The reaction slurry was stirred for 1 hour at 40.degree. C. To the vial was then added 1.6 ml of neat solution of silicon tetrachloride for a total of 13.9 mm. The reaction mixture was stirred for 1 hour at 32.degree. C. The supernatant was decanted and the catalyst dried under flowing nitrogen.

To a 2.1 liter stirred autoclave reactor was charged 850 ml of purified dry hexane. The hexane was heated to 50.degree. C. To this was added 3.6 mm triisobutyl aluminum in 4 ml of hexane solution. A white oil slurry containing 0.25 g of the vanadium containing catalyst (0.05 g/cc) was injected into the reactor via a syringe. 16 mm of Freon-11 activator was then injected into the reactor. The reactor was heated to 85.degree. C., 65 mm H.sub.2 was added, then pressured to a total of 150 psig with ethylene. The polymerization was maintained for 40 minutes at which time the reactor was vented to atmospheric pressure, and the polymer recovered and dried. The polymer had a MI of 0.08, a MIR of 171. The catalyst productivity was 508 g/PE/g catalyst.