Nodular Copolymers Formed of Alpha-Olefin Copolymers Coupled by Non-Conjugated Dienes

The accompanying drawings depict, for illustration purposes only, processes embodied by the present invention, wherein:

FIG. 1 is a schematic representation of a process for producing polymer in accordance with the present invention;

FIG. 2 schematically illustrates how the process depicted in FIG. 1 can be integrated into a lube oil additive process;

FIG. 3 is a graphical illustration of a technique for determining Intra-CD of a polymer;

FIG. 4 graphically illustrates various copolymer structures that can be attained using processes in accordance with the present invention;

FIG. 5 is a schematic representation of the formation of the nodular polymers; and

FIG. 6 illustrates the nodular copolymer which is formed.

As already noted above, the present invention is drawn to novel copolymers of ethylene, at least one other alpha-olefin monomer, and a non-conjugated diene, the copolymers having a MWD prior to coupling characterized by at least one of a M.sub.w /M.sub.n value of less than 2 and a M.sub.z /M.sub.w value of less than 1.8. The copolymer is coupled by reaction of the residual unsaturation of the non-conjugated diene to form the nodular polymers of this invention. More specifically, copolymers in accordance with one embodiment of the present invention comprise intramolecularly heterogeneous chains wherein at least one portion of an individual intramolecularly heterogeneous chain contains only ethylene and alpha-olefin and has a M.sub.w of at least 10.sup.4, and another portion contains ethylene, alpha-olefin, and non-conjugated diene. In the following detailed description of the invention, we use propylene to exemplify the alpha-olefin since it is the most preferred.

Copolymers in accordance with the present invention are preferably made in a tubular reactor. When polymerizing in a tube, the ethylene and propylene are fed to the reactor inlet along with a suitable Ziegler catalyst. The catalyst is preferably chosen so that it produces essentially one active catalyst species. Also, chain transfer reactions during the polymerization must be minimized. It is well known that ethylene is much more readily polymerized than propylene. Consequently, the concentration of monomer changes along the tube in favor of propylene as the ethylene is depleted. The result is copolymer chains which are higher in ethylene content in the chain segments grown near the reactor feed inlet and higher in propylene in the segments grown near the reactor outlet. The resulting chain is intramolecularly heterogeneous. The extent of heterogeneity in ethylene/propylene compositions can be moderated somewhat by feeding additional ethylene at points along the reactor to keep the ethylene/propylene monomer ratio at a more constant value. It is an object of this invention to produce chains with a minimum of interchain compositional variation in order to assure uniform coupling. This is accomplished by utilizing a Ziegler catalyst that forms essentially one active catalyst species, minimizing chain transfer reactions initiating propagation of essentially all chains simultaneously, and conducting the polymerization such that the major portion of the catalyst remains active for the entire length of time that polymerization is occurring in the reactor. The tubular reactor is also operated at conditions such that the copolymer chains have a narrow MWD characterized by at least one of the ratios of M.sub.w /M.sub.n and M.sub.z /Mw being less than 2.0 and 1.8, respectively, prior to coupling.

In one embodiment polymerization of the ethylene and propylene is initiated at the reactor inlet and continued until a first polymer segment forms comprising at least 50% of the weight of the total polymer to be produced. Additional monomer feed is then added to the tube consisting of non-conjugated diene either alone or in combination with the other monomer and/or solvent. at the point of non-conjugated dien addition, at least 50% of the ultimate anticipated mass ot the polymer should have been formed. A second chain segment is then formed with a non-conjugated diene content of at least 0.1 mole % and with a M.sub.w value of at least 2000. If the first polymer segment is formed as a series of discontinuous segments the first segment shall be considered to include the segments as a whole for definitional purposes.

Several techniques are available for producing the nodular branched polymer of this invention. If the non-conjugated diene has both double bonds polymerizable by the Ziegler catalyst, branching will occur simultaneously with polymerization in the reactor. In this case the polymer exiting the reactor will be the final product.

If coupling is to be catalyzed cationically, the cationic catalyst can either be added to the tubular reactor, to carry out the coupling in the reactor, or to the polymer product exiting the reactor so that the coupling can be carried out in a separate process step. Free radical coupling catalysts are normally Ziegler catalyst poisons and will not perform at polymerization conditions. In this case, the coupling agent must be added, and the coupling performed, subsequent to the polymerization. Olefin cross-linking agents may also be used in a similar manner.

Copolymer in accordance with one embodiment of the present invention is preferably made in a tubular reactor. When the process takes place in a tubular reactor, it is known that, at the beginning of the tubular reactor, ethylene, due to its high reactivity, will be preferentially polymerized. However, the concentration of monomers changes along the tube in favor of propylene as the ethylene is depleted. The result is copolymer chains which are higher in ethylene concentration in the chain segments grown near the reactor inlet (as defined at the point at which the polymerization reaction commences), and higher in propylene concentration in the chain segments formed near the reactor outlet. An illustrative copolymer chain of ethylene-proplyene is schematically presented below, with E representing ethylene constituents, and P representing propylene constituents in the chain: ##STR2##

As can be seen from this illustrative schematic chain, the far left-hand segment (1) thereof represents that portion of the chain formed at the reactor inlet where the reaction mixture is proportionately richer in the more reactive constituent ethylene. This segment comprises four ethylene molecules and one propylene molecule. However, as subsequent segments are formed from left to right, with the more reactive ethylene being depleted and the reaction mixture proportionately increasing in propylene concentration, the subsequent chain segments become more concentrated in propylene. The resulting chain is intramolecularly heterogeneous.

In the event that more than two monomers are used, e.g., in the production of EPDM using a diene termonomer, for purposes of describing the present invention all properties related to homogeneity and heterogeneity will refer to the relative ratio of ethylene to the other monomers in the chain. The property, of the copolymer discussed herein, related to intramolecular compositional dispersity (compositional variation within a chain) shall be referred to as Inter-CD.

For copolymer chains in accordance with the present invention, composition can vary between chains as well as along the length of the chain. In one embodiment, an object of this invention is to minimize the amount of interchain variation. The Inter-CD can be characterized by the difference in composition between some fraction of the copolymer and the average composition, as well as by the total difference in composition between the copolymer fractions containing the highest and lowest quantity of ethylene. Techniques for measuring the breadth of the Inter-CD are known, as illustrated by Junghanns et al., wherein a p-xylene-dimethylformamide solvent/non-solvent was used to fractionate copolymer into fractions of differing intermolecular composition. Other solvent/non-solvent systems can be used, such as hexane-2-propanol, as will be discussed in more detail below.

The Inter-CD of copolymer in accordance with one embodiment of the present invention is such that 95 wt. % of the copolymer chains have an ethylene composition that differs from the average weight percent ethylene composition by 15 wt. % or less. The preferred Inter-CD is about 13% or less, with the most preferred being about 10% or less. In comparison, Junghanns et al. found that their tubular reactor copolymer had an Inter-CD of greater than 15 weight %.

Broadly, the Intra-CD of copolymer in accordance with one embodiment of the present invention is such that at least two portions of an individual intramolecularly heterogeneous chain, each portion comprising at least 5 weight percent of the chain, differ in composition from one another by at least 5 weight percent ethylene. Unless otherwise indicated, this property of Intra-CD as referred to herein is based upon at least two 5 weight percent portions of copolymer chain. The Intra-CD of copolymer in accordance with the present invention can be such that at least two portions of copolymer chain differ by at least 10 weight percent ethylene. Differences of at least 20 weight percent ethylene, as well as of at least 40 weight percent ethylene, are also considered to be in accordance with the present invention.

The experimental procedure for determining Intra-CD is as follows. First the Inter-CD is established as described below, then the polymer chain is broken into fragments along its contour and the Inter-CD of the fragments is determined. The difference is the two results is due to Intra-CD, as can be seen in the illustrative example below.

Consider a heterogeneous sample polymer containing 30 monomer units. It consists of 3 molecules designated A, B, C.

A EEEEPEEEPEEEPPEEPPEPPPEPPPPPPP

B EEEEEPEEEPEEEPPEEEPPPEPPPEEPPP

C EEPEEEPEEEPEEEPEEEPPEEPPPEEPPP

Molecule A is 36.8 wt. % ethylene, B is 46.6%, and C is 50% ethylene. The average ethylene content for the mixture is 44.3%. For this sample the Inter-CD is such that the highest ethylene polymer contains 5.7% more ethylene than the average, while the lowest ethylene content polymer contains 7.5% less ethylene than the average. Or, in other words, 100 weight % of the polymer is within +5.7% and -7.5% ethylene about an average of 44.3%. Accordingly, the Inter-CD is 7.5% when the given weight % of the polymer is 100%. The distribution may be represented graphically as by curve 1 in FIG. 3.

If the chains are broken into fragments, there will be a new Inter-CD. For simplicity, consider first breaking only molecule A into fragments shown by the slashes as follows:

Portions of 72.7%, 72.7%, 50%, 30.8%, 14.3% and 0% ethylene are obtained. If molecules B and C are similarly broken and the weight fraction of similar composition are grouped, the new Inter-CD shown by curve 2 in FIG. 3 is obtained. The difference between the two curves in the figure is due to Intra-CD.

Consideration of such data, especially near the end point ranges, demonstrates that for this sample at least 5% of the chain contour represented by the cumulative weight % range (a) differs in composition from another section by at least 15% ethylene shown as (b), the difference between the two curves. The difference in composition represented by (b) cannot be intermolecular. If it were, the separation process for the original polymer would have revealed the higher ethylene contents seen only for the degraded chain.

The compositional differences shown by (b) and (d) in the figure between original and fragmented chains give minimum values for Intra-CD. The Intra-CD must be at least that great, for chain sections have been isolated which are the given difference in composition (b) or (d) from the highest or lowest composition polymer isolated from the original. We know in this example that the original polymer represented at (b) had sections of 72.7% ethylene and 0% ethylene in the same chain. It is highly likely that, due to the inefficiency of the fractionation process, any real polymer with Intra-CD examined will have sections of lower or higher ethylene connected along its contour than that shown by the end points of the fractionation of the original polymer. Thus, this procedure determines a lower bound for Intra-CD. To enhance the detection, the original whole polymer can be fractionated (e.g., separate molecule A from molecule B from molecule C in the hypothetical example) with these fractions refractionated until they show no (or less) Inter-CD. Subsequent fragmentation of this intermolecularly homogeneous fraction now reveals the total Intra-CD. In principle, for the example, if molecule A were isolated, fragmented, fractionated and analyzed, the Intra-CD for the chain sections would be 72.7%-0%=72.7% rather than 72.7%-50%=22.7% seen by fractionating the whole mixture of molecules A, B, and C.

In order to determine the fraction of a polymer which is intramolecularly heterogeneous in a mixture of polymer combined from several sources, the mixture must be separated into fractions which show no further heterogeneity upon subsequent fractionation. These fractions are subsequently fractured and fractionated to reveal polymer heterogeneity.

The fragments into which the original polymer is broken should be large enough to avoid end effects and to give a reasonable opportunity for the normal statistical distribution of segments to form over a given monomer conversion range in the polymerization. Intervals of ca 5 weight % of the polymer are convenient. For example, at an average polymer molecular weight of about 10.sup.5, fragments of ca 5000 molecular weight are appropriate. A detailed mathematical analysis of plug flow or batch polymerization indicates that the rate of change of composition along the polymer chain contour will be most severe at high ethylene conversion near the end of the polymerization. The shortest fragment are needed here to show the low propylene content sections.

The best available technique for determination of compositional dispersity for non-polar polymers is solvent/non-solvent fractionation which is based on the thermodynamics of phase separation. This technique is described in "Polymer Fractionation", M. Cantow editor, Academic 1967, p. 341 ff and in H. Inagaki, T. Tanaku, Developments in Polymer Characterization, 3, 1 (1982). These are incorporated herein by reference.

For non-crystalline copolymers of ethylene and propylene, molecular weight governs insolubility more than does composition in a solvent/non-solvent solution. High molecular weight polymer is less soluble in a given solvent mix. Also, there is a systematic correlation of molecular weight with ethylene content for the polymers described herein. Since ethylene polymerizes much more rapidly than propylene, high ethylene polymer also tends to be high in molecular weight. Additionally, chains rich in ethylene tend to be less soluble in hydrocarbon/polar non-solvent mixture than propylene-rich chains. Thus the high molecular weight, high ethylene chains are easily separated on the basis of thermodynamics.

A fractionation procedure is as follows: Unfragmented polymer is dissolved in n-hexane at 23.degree. C. to form ca a 1% solution (1 g polymer/100 cc hexane). Isopropyl alcohol is titrated into the solution until turbidity appears at which time the precipitate is allowed to settle. The supernatant liquid is removed and the precipitate is dried by pressing between Mylar.RTM. (polyethylene terphthalate) film at 150.degree. C. Ethylene content is determined by ASTM method D-3900. Titration is resumed and subsequent fractions are recovered and analyzed until 100% of the polymer is collected. The titrations are ideally controlled to produce fractions of 5-10% by weight of the original polymer especially at the extremes of composition.

To demonstrate the breadth of the distribution, the data are plotted as % ethylene versus the cumulative weight of polymer as defined by the sum of half the weight % of the fraction of that composition plus the total weight % of the previously collected fractions.

Another portion of the original polymer is broken into fragments. A suitable method for doing this is by thermal degradation according to the following procedure: In a sealed container in a nitrogen-purged oven, a 2 mm thick layer of the polymer is heated for 60 minutes at 330.degree. C. This should be adequate to reduce a 10.sup.5 molecular weight polymer to fragments of ca 5000 molecular weight. Such degradation does not change the average ethylene content of the polymer. This polymer is fractionated by the same procedure as the high molecular weight precursor. Ethylene content is measured, as well as molecular weight on selected fractions.

Ethylene content is measured by ASTM-D3900 for ethylene-propylene copolymers between 35 and 85 wt. % ethylene. Above 85% ASTM-D2238 can be used to obtain methyl group concentrations which are related to percent ethylene in an unambiguous manner for ethylene-propylene copolymers. When comonomers other than propylene are employed, no ASTM tests covering a wide range of ethylene contents are available; however, proton and carbon 13 nuclear magnetic resonance can be employed to determine the composition of such polymers. These are absolute techniques requiring no calibration when operated such that all nuclei contribute equally to the spectra. For ranges not covered by the ASTM tests for ethylene-propylene copolymers, these nuclear magnetic resonance methods can also be used.

Molecular weight and molecular weight distribution are measured using the Waters 150 gel permeation chromtograph equipped with a Chromatix KMX-6 on-line light scattering photometer. The system is used at 135.degree. C. with 1, 2, 4-trichlorobenzene as mobile phase. Showdex (Showa-Denko America, Inc.) polystyrene gel columns 802, 803, 804 and 805 are used. This technique is discussed in "Liquid Chromtography of Polymers and Related Material III", J. Cazes editor, Marcel Dekker, 1981, p. 207 (incorporated herein by reference). No corrections for column spreading are employed; however, data on generally accepted standards, e.g., National Bureau of Standards Polyethene 1484 and anionically produced hydrogenated polyisoprenes (an alternating ethylene-propylene copolymer) demonstrate that such corrections on M.sub.w /M.sub.n or M.sub.z /M.sub.w are less than 0.05 unit. M.sub.w /M.sub.n is calculated from an elution time-molecular weight relationship whereas M.sub.z /M.sub.w is evaluated using the light scattering photometer. The numerical analyses can be performed using the commercially available computer software GPC2, MOLWT2 available from LDC/Milton Roy-Riviera Beach, Fla.

As already noted, the first copolymer segment in accordance with the present invention is comprised of ethylene and at least one other alpha-olefin. It is believed that such alpha-olefins could include those containing 3 to 18 carbon atoms, e.g., propylene, butene-1, pentene-1, etc. Alpha-olefins of 3 to 6 carbons are preferred due to economic considerations. The most preferred alpha-olefin in accordance with the present invention is propylene.

The diene monomers suitable for use in the practice of this invention by which the narrow MWD polymers prepared by this invention are coupled, are of two types: (1) non-conjugated dienes capable of being Ziegler catalyst polymerized via both double bonds; and (2) the non-conjugated dienes of the type used to prepare EPDM where the non-conjugated diene has only one Ziegler catalyst polymerizable double bond and the other bond is cross-linkable by cationic or free radical catalysts or by olefin cross-linking agents.

Typical of the coupling agents that can be used to produce the second terpolymer segment of the chain are the following non-limiting examples:

(a) straight chain acyclic dienes such as: 1,4-hexadiene; 1,6-octadiene;

(b) branched chain acyclic dienes such as: 5-methyl-1, 4-hexadiene; 3,7-dimethyl-1,6-octadiene; 3,7-dimethyl-1,7-octadiene; 3,7-dimethyl-1,7-Octadine and the mixed isomers of dihydromyrcene and dihydroocinene;

(c) single ring alicyclic dienes such as: 1,4-cyclohexadiene; 1,5-cyclooctoadiene; and 1,5-cyclododecadiene

(d) multi-ring alicyclic fused and bridged ring dienes such as: tetrahydroindene; methyltetrahydroindene; dicyclopentadiene; bicyclo-(2,2,1)-hepta-2,5 diene; alkenyl, alkylidene, cycloalkenyl and cycloalkylidene norbornenes such as 5-methylene-2-norbornene (MNB), 5-ethylidene-2-norbornene (ENB), 5-propyl-2-norbornene, 5-isopropylidene-2-norbornene, 5-(4-cyclopentenyl)-2-norbornene; 5-cyclohexylidene-2-norbornene.

Illustrative, non-limiting examples of the diene monomers coupled by Ziegler copolymerization catalysts to prepare the nodular polymers of this invention are norbornadiene, vinyl norbornene and butenyl norbornene. Illustrative of the dienes coupled by cationic cross-linkable catalysis to prepare the nodular polymers are 1,4-hexadiene, ENB, and dicyclopentadiene. Illustrative of the dienes coupled by free radical catalysts are MNB, VNB, and 1,5-hexadiene. Additionally, olefin cross-linking agents may be used. Such agents include sulfur dichloride, disulfenyl halides, borane, dithioalkenes, and mixtures thereof. Of the non-conjugated dienes typically used to prepare these copolymers, dienes containing at least one of the double bonds in a strained ring are preferred. The amount of diene (mol basis) in the diene-containing segment of the polymer could be from about 0.1% mole to 50%, with 1% to 30% being preferred. The most preferred range is 2%-20%.

The average ethylene content of the polymer could be as low as about 10% on a weight basis. The preferred minimum is about 25%. A more preferred minimum is about 30%. The maximum ethylene content could be about 90% on a weight basis. The preferred maximum is about 85%, with the most preferred being about 80%. The ethylene content of the two segments comprising the polymer can be the same or different. If different, the preferred composition range for each segment is the same as stated above for the whole polymer.

The molecular weight of copolymer made in accordance with the present invention can vary over a wide range. It is believed that the weight average molecular weight could be as low as about 2,000. The preferred minimum is about 10,000. The most preferred minimum is about 20,000. It is believed that the maximum weight average molecular weight could be as high as about 12,000,000. The preferred maximum is about 1,000,000. The most preferred maximum is about 750,000. The preferred minimum molecular weight for an ethylene-propylene copolymer chain segment is 2.times.10.sup.4. For the ethylene-propylene-non-conjugated diene chain segment the preferred minimum MW is 2.times.10.sup.3.

Another feature of polymer made in accordance with the present invention is that the molecular weight distribution (MWD) prior to coupling is very narrow, as characterized by at least one of a ratio of M.sub.w /M.sub.n of less than 2 and a ratio of M.sub.z /M.sub.w of less than 1.8 for the whole polymer and the first chain segment. Some typical advantages of such polymers having narrow MWD both before and after coupling are greater resistance to shear degradation. Particularly for oil additive applications, the preferred uncoupled copolymers have M.sub.w /M.sub.n less than about 1.6, with less than about 1.4 being most preferred. The preferred M.sub.z /M.sub.w is less than about 1.5, with less than about 1.3 being most preferred. The addition of diene to produce branched structures is known. However, by coupling narrow MWD polymers only near their ends, more shear stable structures are produced than by random coupling, both as a result of more favorable stress distribution in the polymer in service and less MWD broadening than in random coupling as in prior art methods.

Solution polymerizations are preferred for the polymerization process of this invention. Any known solvent for the reaction mixture that is effective for the purpose can be used. For example, suitable solvents would be hydrocarbon solvents such as aliphatic, cycloaliphatic and aromatic hydrocarbon solvents, or halogenated versions of such solvents. The preferred solvents are C.sub.12 or lower, straight chain or branched chain, saturated hydrocarbons, C.sub.5 to C.sub.9 saturated alicyclic or aromatic hydrocarbons or C.sub.2 to C.sub.6 halogenated hydrocarbons. Most preferred are C.sub.12 or lower, straight chain or branched chain hydrocarbons, particularly hexane. Nonlimiting illustrative examples of solvents are butane, pentane, hexane, heptane, cyclopentane, cyclohexane, cycloheptane, methyl cyclopentane, methyl cyclohexane, isoctane, benzene, toluene, xylene, chloroform, chlorobenzenes, tetrachloroethylene, dichlorethane and trichloroethane.

The polymerization process is preferably carried out in a mix-free reactor system, which is one in which substantially no mixing occurs between portions of the reaction mixture that contain polymer chains initiating at different times. Suitable reactors are a continuous flow tubular or a stirred batch reactor. A tubular reactor is well known and is designed to minimize mixing of the reactants in the direction of flow. As a result, reactant concentration will vary along the reactor length. In contrast, the reaction mixture in a continuous flow stirred tank reactor (CFSTR) is blended with the incoming feed to produce a solution of essentially uniform composition everywhere in the reactor. Consequently, the growing chains in a portion of the reaction mixture will have a variety of ages and thus a single CFSTR is not suitable for the process of this invention. However, it is well known that 3 or more stirred tanks in series with all of the catalyst fed to the first reactor can approximate the performance of a tubular reactor. Accordingly, such tanks in series are considered to be in accordance with the present invention, and as being the functional equivalent of the tubular reactor.

A batch reactor is a suitable vessel, preferably equipped with adequate agitation, to which the catalyst, solvent, and monomer are added at the start of the polymerization. The charge of reactants is then left to polymerize for a time long enough to produce the desired product. For economic reasons, a tubular reactor is preferred to a batch reactor for carrying out the processes of this invention.

In addition to the importance of the reactor system to make copolymers in accordance with the present invention, the polymerization should be preferably conducted such that:

a. the catalyst system produces essentially one active catalyst species,

b. the reaction mixture is essentially free of chain transfer agents, and

c. the polymer chains are essentially all initiated simultaneously, which is at the same time for a batch reactor or at the same point along the length of the tube for a tubular reactor.

The desired polymer can be obtained if more than one feed or solvent and reactants (e.g., at least one of the ethylene, alpha-olefin and diene) are added either at at least one point along the length of a tubular reactor or during the course of polymerization in a batch reactor. Operating in this fashion may be desirable in certain circumstances to control the polymerization rate or polymer composition. However, it is necessary to add essentially all of the catalyst at the inlet of the tube or at the onset of batch reactor operation to meet the requirement that essentially all polymer chains are initiated simultaneously.

Accordingly, processes in accordance with the present invention are most preferably carried out:

(a) in at least one mix-free reactor,

(b) using a catalyst system that produces essentially one active catalyst species,

(c) using at least one reaction mixture which is essentially transfer agent-free, and

(d) in such a manner and under conditions sufficient to initiate propagation of essentially all polymer chains simultaneously.

Since the tubular reactor is the preferred reactor system for carrying out processes in accordance with the present invention, the following illustrative descriptions and examples are drawn to that system, but will apply to other reactor systems as will readily occur to the artisan having the benefit of the present disclosure.

In practicing processes in accordance with the present invention, use is preferably made of at least one tubular reactor. Thus, in its simplest form, such a process would make use of but a single reactor. However, as would readily occur to the artisan having the benefit of the present disclosure, more than one reactor could be used, either in parallel for economic reasons, or in series with multiple monomer feed to vary intramolecular composition.

For example, various structures can be prepared by adding additional monomer(s) during the course of the polymerization. This is exemplified in FIG. 4, wherein composition is plotted versus position along the contour length of the chain for multiple monomer additions during polymerization of the ethylene-propylene copolymer chain segment. The Intra-CD of curve 1 is obtained by feeding all of the monomers at the tubular reactor inlet or at the start of a batch reaction. In comparison, the Intra-CD of curve 2 can be made by adding additional ethylene at a point along the tube, or, in a batch reactor, where the chains have reached about half their length. The Intra-CD's of curve 3 requires multiple feed additions. The Intra-CD of curve 4 can be formed if additional comonomer rather than ethylene is added. This structure permits a whole ethylene composition range to be omitted from the chain. In each case, a third or more alpha-olefin comonomers may be added.

The composition of the catalyst used to produce alpha-olefin copolymers has a profound effect on copolymer product properties such as compositional dispersity and MWD. The catalyst utilized in practicing processes in accordance with the present invention should be such as to yield essentially one active catalyst species in the reaction mixture. More specifically, it should yield one primary active catalyst species which provides for substantially all of the polymerization reaction. Additional active catalyst species could be present, provided the copolymer product is in accordance with the present invention, e.g., narrow MWD and Inter-CD. It is believed that such additional active catalyst species could provide as much as 35% (weight) of the total copolymer. Preferably, they should account for about 10% or less of the copolymer. Thus, the essentially one active species should provide for at least 65% of the total copolymer produced, preferably for at least 90% thereof. The extent to which a catalyst species contributes to the polymerization can be readily determined using the below-described techniques for characterizing catalyst according to the number of active catalyst species.

Techniques for characterizing catalyst according to the number of active catalyst species are within the skill of the art, as evidenced by an article entitled "Ethylene-Propylene Copolymers. Reactivity Ratios, Evaluation and Significance", C. Cozewith and G. VerStrate, Macromolecules, 4,482 (1971), which is incorporated herein by reference.

It is disclosed by the authors that copolymers made in a continuous flow stirred reactor should have an MWD characterized by M.sub.w /M.sub.n =2 and a narrow Inter-CD when one active catalyst species is present. By a combination of fractionation and gel permeation chromatography (GPC) it is shown that for single active species catalysts the composition of the fractions vary no more than .+-.3% about the average and the MWD (weight to number average ratio) for these samples approaches two (2). It is this latter characteristic (M.sub.w /M.sub.n of about 2) that is deemed the more important in identifying a single active catalyst species. On the other hand, other catalysts gave copolymer with an Inter-CD greater than .+-.10% about the average, and multimodal MWD with a M.sub.w /M.sub.n value greater than about 2. These other catalysts are deemed to have more than one active species.

Catalyst systems to be used in carrying out processes in accordance with the present invention may be Ziegler copolymerization catalysts, which may typically include:

(a) a compound of a transition metal, i.e., a metal of Groups I-B, III-B, IVB, VB, VIB, VIIB, and VIII of the Periodic Table, and

(b) an organometal compound of a metal of Groups I-A, II-A, II-B, and III-A of the Periodic Table.

The preferred catalyst system in practicing processes in accordance with the present invention comprises hydrocarbon-soluble vanadium compound in which the vanadium valence is 3 to 5 and organo-aluminum compound, with the provision that the catalyst system yields essentially one active catalyst species as described above. At least one of the vanadium compound/organo-aluminum pair selected must also contain a valence-bonded halogen.

In terms of formulas, vanadium compounds useful in practicing processes in accordance with the present invention could be: ##STR3## where x=0-3 and R=a hydrocarbon radical; VCl.sub.4 ;

VO(AcAc).sub.2, where AcAc.dbd.acetyl acetonate;

V(AcAc).sub.3 ;

where x=1 or 2; and

VCl.sub.3.nB where n=2-3 and B=Lewis base capable of making hydrocarbon-soluble complexes with VCl.sub.3, such as tetrahydrofuran, 2-methyl-tetrahydrofuran and dimethyl pyridine.

In formula 1 above, R preferably represents a C.sub.1 to C.sub.10 aliphatic, alicyclic or aromatic hydrocarbon radical such as ethyl (Et), phenyl, isopropyl, butyl, propyl, n-butyl, i-butyl, t-butyl, hexyl, cyclohexyl, octyl, naphthyl, etc. Non-limiting illustrative examples of formula (1) and (2) compounds are vanadyl trihalides, alkoxy halides and alkoxides such as VOCl.sub.3, VOCl.sub.2 (OBu) where Bu=butyl, and VO(OC.sub.2 H.sub.5).sub.3. The most preferred vanadium compounds are VCl.sub.4, VOCl.sub.3, and VOCl.sub.2 (OR).

As already noted, the co-catalyst is preferably organo-aluminum compound. In terms of chemical formulas, these compounds could be as follows: ##STR4## where R and R' represent hydrocarbon radicals, the same or different, as described above with respect to the vanadium compound formula. The most preferred organo-aluminum compound is an aluminum alkyl sesquichloride such as Al.sub.2 Et.sub.3 Cl.sub.3 or Al.sub.2 (iBu).sub.3 Cl.sub.3.

In terms of performance, a catalyst system comprised of VCl.sub.4 and Al.sub.2 R.sub.3 Cl.sub.3, preferably where R is ethyl, has been shown to be particularly effective. For best catalyst performance, the molar amounts of catalyst components added to the reaction mixture should provide a molar ratio of aluminum/vanadium (Al/V) of at least about 2. The preferred minimum Al/V is about 4. The maximum Al/V is based primarily on the considerations of catalyst expense and the desire to minimize the amount of chain transfer that may be caused by the organo-aluminum compound (as explained in detail below). Since, as is known, certain organo-aluminum compounds act as chain transfer agents, if too much is present in the reaction mixture the M.sub.w /M.sub.n of the copolymer may rise above 2. Based on these considerations, the maximum Al/V could be about 25; however, a maximum of about 17 is more preferred. The most preferred maximum is about 15.

Chain transfer agents for the Ziegler-catalyzed polymerization of alpha-olefins are well known and are illustrated, by way of example, by hydrogen or diethyl zinc for the production of EPM and EPDM. Such agents are very commonly used to control the molecular weight of EPM and EPDM produced in continuous flow stirred reactors. For the essentially single active species Ziegler catalyst systems used in accordance with the present invention, addition of chain transfer agents to a CFSTR reduces the polymer molecular weight but does not affect the molecular weight distribution. On the other hand, chain transfer reactions during tubular reactor polymerization in accordance with the present invention broaden polymer molecular weight distribution.

Chains which terminate prior to addition of the nonconjugated diene will not be coupled into the nodular structure. Thus, the presence of chain transfer agents in the reaction mixture should be minimized or omitted altogether. Although difficult to generalize for all possible reactions, the amount of chain transfer agent used should be limited to those amounts that provide copolymer product in accordance with the desired limits as regards MWD and compositional dispersity. It is believed that the maximum amount of chain transfer agent present in the reaction mixture could be as high as about 0.2 mol/mol of transition metal, e.g., vanadium, again provided that the resulting copolymer product is in accordance with the desired limits as regards MWD and compositional dispersity. Even in the absence of added chain transfer agent, chain transfer reactions can occur because propylene and the organo-aluminum co-catalyst can also act as chain transfer agents. In general, among the organo-aluminum compounds that in combination with the vanadium compound yield just one active species, the organo-aluminum compound that gives the highest copolymer molecular weight at acceptable catalyst activity should be chosen. Furthermore, if the Al/V ratio has an effect on the molecular weight of copolymer product, that Al/V should be used which gives the highest molecular weight also at acceptable catalyst activity. Chain transfer with propylene can best be limited by avoiding excessive temperature during the polymerization as described below.

Molecular weight distribution and Inter-CD are also broadened by catalyst deactivation during the course of the polymerization which leads to termination of growing chains. It is well known that the vanadium-based Ziegler catalysts used in accordance with the present invention are subject to such deactivation reactions which depend to an extent upon the composition of the catalyst. Although the relationship between active catalyst lifetime and catalyst system composition is not known at present, for any given catalyst, deactivation can be reduced by using the shortest residence time and lowest temperature in the reactor that will produce the desired monomer conversions.

When catalyst deactivation is occurring, the feed containing diene monomer is preferably added to the reactor at a point during the polymerization where at least 50% of the catalyst is still active. Polymerizations in accordance with the present invention should be conducted in such a manner and under conditions sufficient to initiate propagation of essentially all copolymer chains simultaneously. This can be accomplished by utilizing the process steps and conditions described below.

The catalyst components are preferably premixed, that is, reacted to form active catalyst outside of the reactor, to ensure rapid chain initiation. Aging of the premixed catalyst system, that is, the time spent by the catalyst components (e.g., vanadium compound and organo-aluminum) in each other's presence outside of the reactor, should preferably be kept within limits. If not aged for a sufficient period of time, the components will not have reacted with each other sufficiently to yield an adequate quantity of active catalyst species, with the result of nonsimultaneous chain initiation. Also, it is known that the activity of the catalyst species will decrease with time so that the aging must be kept below a maximum limit. It is believed that the minimum aging period, depending on such factors as concentration of catalyst components, temperature and mixing equipment could be as low as about 0.1 second.

The preferred minimum aging period is about 0.5 second, while the most preferred minimum aging period is about 1 second. The vanadium/organo-aluminum catalyst system can be aged indefinitely. While the maximum aging period could be higher, for the preferred vanadium/organo-aluminum catalyst system the preferred maximum is at least 500 seconds and possibly about 5000 seconds. A more preferred maximum is about 200 seconds. The most preferred maximum aging period is about 100 seconds. The premixing could be performed at a low temperature such as 40.degree. C. or below. It is preferred that the premixing be performed at 25.degree. C. or below, with 15.degree. or below being most preferred.

The temperature of the reaction mixture should also be kept within certain limits. The temperature at the reactor inlet should be high enough to provide complete, rapid chain initiation at the start of the polymerization reaction. The length of time that the reaction mixture spends at high temperature must be short enough to minimize the amount of undesirable chain transfer and catalyst deactivation reactions.

Temperature control of the reaction mixture is complicated somewhat by the fact that the polymerization reaction generates large quantities of heat. This problem is, preferably, taken care of by using prechilled feed to the reactor to absorb the heat of polymerization. With this technique, the reactor is operated adiabatically and the temperature is allowed to increase during the course of polymerization. As an alternative to feed prechill, heat can be removed from the reaction mixture, for example, by a heat exchanger surrounding at least a portion of the reactor or by well-known autorefrigeration techniques in the case of batch reactors or multiple stirred reactors in series.

If adiabatic reactor operation is used, the inlet temperature of the reactor feed could be about from -50.degree. C. to 140.degree. C. It is believed that the outlet temperature of the reaction mixture could be as high as about 150.degree. C. The preferred maximum outlet temperature is about 70.degree. C. The most preferred maximum is about 50.degree. C. In the absence of reactor cooling, such as by a cooling jacket, to remove the heat of polymerization, the temperature of the reaction mixture will increase from reactor inlet to outlet by an amount dependant on the heat of polymerization, reaction mixture specific heat, and the weight percent of copolymer in the reaction mixture. For ethylene-propylene copolymerization in hexane solvent the temperature rise is about 13 degrees C. per weight percent of copolymer formed.

Having the benefit of the above disclosure, it would be well within the skill of the art to determine the operating temperature conditions for making copolymer in accordance with the present invention. For example, assume an adiabatic reactor and an outlet temperature of 35.degree. C. are desired for a reaction mixture containing 5% copolymer. The reaction mixture will increase in temperature by about 13.degree. C. for each weight percent copolymer or 5 weight percent x 10.degree. C./wt. %=50.degree. C. To maintain an outlet temperature of 35.degree. C., it will thus require a feed that has been prechilled to 35.degree. C.-50.degree. C.=-15.degree. C. In the instance that external cooling is used to absorb the heat of polymerization, the feed inlet temperature could be higher with the other temperature constraints described above otherwise being applicable.

Because of heat removal and reactor temperature limitations, the preferred maximum copolymer concentration at the reactor outlet is 25 wt./100 wt. diluent. The most preferred maximum concentration is 15 wt./100 wt. There is no lower limit to concentration due to reactor operability, but for economic reasons, it is preferred to have a copolymer concentration of at least 2 wt./100 wt. Most preferred is a concentration of at least 3 wt./100 wt.

The rate of flow of the reaction mixture through the reactor should be high enough to provide good mixing of the reactants in the radial direction and minimize mixing in the axial direction. Good radial mixing is beneficial not only to both the Intra- and Inter-CD of the copolymer chains, but also to minimize radial temperature gradients due to the heat generated by the polymerization reaction. Radial temperature gradients will tend to broaden the molecular weight distribution of the copolymer, since the polymerization rate is faster in the high temperature regions resulting from poor heat dissipation. The artisan will recognize that achievement of these objectives is difficult in the case of highly viscous solutions. This problem can be overcome to some extent through the use of radial mixing devices such as static mixers (e.g., those produced by the Kenics Corporation).

It is believed that residence time of the reaction mixture in the mix-free reactor can vary over a wide range. It is believed that the minimum could be as low as about 1 second. A preferred minimum is about 10 seconds. The most preferred minimum is about 15 seconds. It is believed that the maximum could be as high as about 3600 seconds. A preferred maximum is about 1800 seconds. The most preferred maximum is about 900 seconds.

With reference to the accompanying drawings, particularly FIG. 1, reference numeral 1 generally refers to a premixing device for premixing the catalyst components. For purposes of illustration, it is assumed that the copolymer of ethylene and propylene (EPM) is to be produced using as catalyst components vanadium tetrachloride and ethyl aluminum sesquichloride. The polymerization is an adiabatic, solution polymerization process using hexane solvent for both the catalyst system and the reaction mixture.

The premixing device 1 comprises a temperature control bath 2, a fluid flow conduit 3 and mixing device 4 (e.g., a mixing tee). To mixing device 4 are fed hexane solvent, vanadium tetrachloride and ethyl aluminum sesquichloride through feed conduits 5, 6 and 7, respectively. Upon being mixed in mixing device 4, the resulting catalyst mixture is caused to flow within conduit 3, optionally in the form of a coiled tube, for a time long enough to produce the active catalyst species at the temperature set by the temperature bath. The temperature of the bath is set to give the desired catalyst solution temperature in conduit 3 at the outlet of the bath.

Upon leaving the premixing device, the catalyst solution flows through conduit 8 into mixing zone 9 to provide an intimate mixing with hexane solvent and reactants (ethylene and propylene) which are fed through conduit 10. Any suitable mixing device can be used, such as a mechanical mixer, orifice mixer or mixing tee. For economic reasons, the mixing tee is preferred. The residence time of the reaction mixture in mixing zone 9 is kept short enough to prevent significant polymer formation therein before being fed through conduit 11 to the first section of the tubular reactor, 12. Alternatively, streams 8 and 10 can be fed directly to the inlet of reactor 12 if the flow rates are high enough to accomplish the desired level of intimate mixing. The hexane with dissolved monomers may be cooled upstream of mixing zone 9 to provide the desired feed temperature at the reactor inlet.

At the outlet of the tubular reactor, A, the polymer solvent and unreacted monomer enter mixer 13 through inlet line 14, where the diene and, optionally, additional monomers are introduced. After mixing, the polymer solution and additional monomer feed pass into the second stage of the tubular reactor, 15, where polymerization continues. For Ziegler copolymerizable dienes or dienes coupled by cationic catalysts, coupling to form the nodular polymer of this invention may also occur in reactor 15. The polymer/solvent mixture with unreacted monomer exits the reactor, 15, at point B, where it is collected for treatment and recovery. If the polymer remains uncoupled at point B such treatment includes the addition of suitable crosslinking agents to form the nodular polymer. While the reactor can be operated adiabatically, if desired or necessary to maintain the reaction mixture temperature within desired limits, external cooling means such as a cooling jacket surrounding at least a portion of the reactor system, 12, and 15, can be provided.

In one embodiment, the process of this invention is carried out by beginning the polymerization of the poly co(ethylene-propylene) which is permitted to grow to a molecular weight of several tens of thousands, e.g., 10,000 to 50,000 number average molecular weight. The polymerization of the copolymer will generally have proceeded to about 50% of the total anticipated weight of polymer at the end of polymerization, more preferably at least 70% of the total weight; at that point in time, the diene monomer, and optionally, a cationic catalyst if the diene is subject to cationically catalyzed coupling are introduced into the reactor with or without additional ethylene and propylene. With Ziegler copolymerizable dienes the polymer copolymerizes with the double bonds of the diene monomer to form the nodular polymers of this invention. This diolefin copolymerizes at the chain ends coupling several chains, as illustrated schematically in FIG. 5. Alternatively, coupling agent may be added at the entrance to the tubular reactor with a part of the ethylene and alpha-olefin monomer, polymerization being carried out until nodules are formed and the coupling agent is substantially converted; then additional ethylene and alpha-olefin are added to grow nodular polymers of this invention.

With reference to FIG. 2, which schematically illustrates a process for mixing nodular copolymer with lube oil, a nodular copolymer product from reactor 15 is fed through conduit 16 to deashing section 17, wherein catalyst residues are removed from the reaction mixture in a known manner (known as deashing). The vanadium and aluminum compound residues are removed by reacting them with water to form hydrocarbon-isoluble hydroxides, and then extracting the hydroxides into dilute acid.

After separating the aqueous and hydrocarbon phases, for instance in a gravity settler, the polymer solution, which primarily contains solvent, unreacted monomers and copolymer product (EPM), is fed through conduit 18 to lube oil mixing tank 19. Of course, tank 19 could be a staged series of tanks. Hot lube oil is fed through conduit 20 to mixing tank 19, wherein the remaining reaction mixture is heated up such that the remaining hexane and unreacted monomers are vaporized and removed through recycle conduit 21, through which they flow back for reuse in premixing device 1 following suitable purification, to remove any catalyst poisons. The copolymer product, being hydrocarbon-soluble, is now present in the lube oil and is removed from tank 19 as a copolymer-in-oil solution.

Alternatively, the copolymer solution from the gravity settler can be stream distilled with subsequent extrusion drying of the polymer, and then mixed with a hydrocarbon mineral oil diluent to produce an oil additive concentrate or lube oil additive.

Having thus described the above illustrative reactor system, it will readily occur to the artisan that many variations can be made within the scope of the present invention. For example, the placement and number of multiple feed sites, the choice of temperature profile during polymerization, and the concentrations of reactants can be varied to suit the end-use application.

By practicing processes in accordance with the present invention, alpha-olefin copolymers having very narrow MWD can be made by direct polymerization and coupled to form nodular polymers.

A lubricating oil composition in accordance with the present invention comprises a major amount of basestock lubricating oil (lube oil) of lubricating viscosity which contains an effective amount of Viscosity Index improver being a nodular copolymer of ethylene and at least one other alpha-olefin, as described in detail above. More specifically, the chains coupled to form the nodular copolymer should have a MWD characterized by at least one of a ratio of M.sub.w /M.sub.n of less than 2 and a ratio of M.sub.z /M.sub.w of less than 1.8. The preferred ratio of M.sub.w /M.sub.n is less than about 1.6, with less than about 1.4 being preferred. The preferred M.sub.z /M.sub.w is less than about 1.5, with less than about 1.3 being most preferred.

In one embodiment of the invention, the Intra-CD of the copolymer is such that at least two portions of an individual intramolecularly hetrogeneous chain, each portion comprising at least 5 weight percent of the chain, differ in composition from one another by at least 5 weight percent ethylene. The Intra-CD can be such that at least two portions of copolymer chain differ by at least 10 weight percent ethylene. Difference of at least 20 weight percent, as well as 40 weight percent ethylene, are also considered to be in accordance with the present invention.

In another embodiment of the invention, the Inter-CD of the copolymer is such that 95 wt. % of the copolymer chains have an ethylene composition that differs from the copolymer average weight percent ethylene composition by 15 wt. % or less. The preferred Inter-CD is about 13% or less, with the most preferred being about 10% or less.

In a particular embodiment, the copolymer has all of the MWD, Intra-CD and Inter-CD characteristics described above when incorporated in a lubricating oil or oil additive concentrate composition. In current practice, ethylenepropylene copolymer is most preferred. The preferred ethylene content of the copolymer, on a weight basis, for use as a lube oil additive is about from 30% to 75%.

For lube oil additive applications, it is believed that the copolymer could have a weight average molecular weight as low as about 2,000. The preferred minimum is about 15,000, with about 50,000 being the most preferred minimum. It is believed that the maximum weight average molecular weight could be as high as about 12,000,000. The preferred maximum is about 300,000, with about 250,000 being the most preferred maximum. The preferred ethylene content is 30% to 75%.

The nodular copolymers of this invention may be employed in lubricating oils as Viscosity Index improvers or viscosity modifiers in amounts varying broadly from about 0.001 to 49 wt. %. The proportions giving the best results will vary somewhat according to the nature of the lubricating oil basestock and the specific purpose for which the lubricant is to serve in a given case. When used as lubricating oils for diesel or gasoline engine crankcase lubricants, the polymer concentrations are within the range of about 0.1 to 15.0 wt. % of the total composition, which are amounts effective to provide Viscosity Index improvements. Typically, such polymeric additives are sold as oil additive concentrates wherein the additive is present in amounts of about 5 to 50 wt. %, preferably 6 to 25 wt. % based on the total amount of hydrocarbon mineral oil diluent for the additive. The polymers of this invention are typically used in lubricating oils based on a hydrocarbon mineral oil having a viscosity of about 2-40 centistokes (ASTM D-445) at 99.degree. C.; however, lubricating oil basestocks comprised of a mixture of a hydrocarbon mineral oil and up to about 25 wt. % of a synthetic lubricating oil, such as esters of dibasic acids and complex esters derived from monobasic acids, polyglycols, dibasic acids and alcohols, are also considered suitable.

The novel compositions of this invention comprise about .05 to about 25 mol % coupling agent based on the total nodular polymer, preferably about 0.1 to about 15 mol %, more preferably about 0.15 to about 10 mol %. In the process for preparing the nodular copolymer, the coupling agent is preferably utilized in the reaction mixture at about 0.1 to about 80 wt. % based on the total monomer, more preferably about 0.5 to about 50 wt. %. The most preferred range is 2% to 20%.

The novel process to form the nodular polymers of this invention may be more readily appreciated by reference to the following examples.

Solution polymerization of ethylene, propylene and norbornadiene was carried out in a tubular reactor with VCl.sub.4 catalyst and Al.sub.2 Et.sub.3 Cl.sub.3 (EASC) cocatalyst as the catalyst system. Norbornadiene (NBD) is a Ziegler copolymerizable diene that yields a nodular copolymer in the presence of the VCl.sub.4 /EASC catalyst system. The polymerization equipment is shown in FIG. 1. The catalyst and co-catalyst were premixed as dilute solutions in hexane for about 6 sec. at 0.degree. C. The catalyst was combined with chilled hexane, ethylene, and propylene at a temperature of -10.degree. C. in mixing zone 9. The reaction mixture then entered reactor 12. At point 13 along the reactor, norbornadiene was fed dissolved in hexane with varying amounts of ethylene through line 14. The reactor residence time was 40 sec. The polymerization was conducted adiabatically to give a reactor outlet temperature of about 40.degree. C.

The polymerization was terminated by quenching the catalyst with water and the polymer was recovered from solution by steam stripping to remove the hexane followed by drying the polymer on a hot rubber mill. Characteristics of the polymerization prior to point 13 were measured by removing small polymer solution samples and determining the polymer concentration.

As shown by the results 1A, 1B and 1C in Table I, increasing the ethylene feed rate at point 13 increases the NBD content of the polymer and thereby the amount of chain coupling as measured by the increase in Mooney viscosity (ML) and bulk viscosity (No). The viscosity ratio, which measures the amount of chain coupling by comparing the viscosity of the branched and an unbranched copolymer of the same M.sub.w, also increases substantially.

The procedure of Example 1 was repeated except ethylidene norbornene (ENB) was added at point 13. ENB is a cross-linkable diene that gives chain coupling in the presence of a Lewis acid such as EASC which is present as part of the catalyst system. As shown in Table I, the nodular polymer produced has an enhanced viscosity ratio.

Polymerization in a tubular reactor is carried out with VCl.sub.4 catalyst and diisobutyl aluminum chloride (DIBAC) cocatalyst as the catalyst system. The components are premixed for 1 sec. at 0.degree. C. and combined with a hexane, ethylene, and propylene solution at 0.degree. C. at the reactor inlet. ENB, ethylene, and hexane are fed at point 13 along the reactor to form a second chain segment containing coupling agent. Feed rates are shown in Table I. The polymer solution exiting the reactor is substantially uncoupled. The solution is subjected to reduced pressure to strip off most of the unreacted monomers and then a solution of ethyl aluminum dichloride, a Lewis acid catalyst, is added to couple the chains by crosslinking. The product is recovered by aqueous deashing to remove catalyst residues followed by steam stripping to remove the solvent, and extrusion drying of the polymer.

The procedure of Example 3 is repeated in a tubular reactor containing two additional inlets downstream of the point 13 shown in FIG. 1. An additional monomer feed of 50 g/hr of ethylene dissolved in hexane is added at the first of these inlets to increase the extent of ENB incorporation into the growing copolymer chains, and the polymerization is allowed to proceed until substantially all of the ENB is converted. A feed of 100 g/hr of ethylene, 500 g/hr propylene and 6 l/hr of hexane is fed at the second inlet to form a chain segment containing essentially only ethylene and propylene. The polymer exiting the reactor is substantially uncrosslinked and has a narrow MWD characterized by M.sub.w /M.sub.n =1.5. The chains consist of an initial and final section containing only ethylene and propylene and a central section containing ENB. A nodular copolymer is produced by the procedure described in Example 3.

Polymerization in a tubular reactor is carried out with VCl.sub.4 catalyst and EASC cocatalyst as the catalyst system, premixed as described in Example 1. The catalyst stream is combined at the reactor inlet with a monomer feed of ethylene, propylene, and vinyl norbornene dissolved in hexane. Vinyl norbornene is a Ziegler copolymerizable diene that produces coupled chains in the presence of the catalyst system. Feed rates are as shown in Table I. After a reaction time sufficient to produce high diene conversion, ethylene, propylene and additional hexane are added at point 13 along the reactor. The polymerization is quenched with water at the end of the reactor and the polymer is recovered by usual means. The product is a nodular copolymer having a high viscosity ratio.

Polymerization of monomer is carried out as described in Example 3 to produce a solution of uncoupled polymer chains. This solution is fed to an agitated vessel maintained at 25.degree. C. temperature along with SCl.sub.2. The SCl.sub.2 feed rate is set at 1.2 mol/mol of double bonds available in the polymer. Chain coupling takes place in a residence time of 10 minutes. The polymer is recovered from the solution by steam stripping and extrusion drying to yield a nodular copolymer product.

The polymerization of Example 3 is repeated except isopropylidene norbornene is fed to the reactor instead of ENB and the feed rates are as shown in Table I. The polymer chains leaving the reactor are substantially uncoupled. The polymer is recovered from solution by steam stripping followed by extrusion drying. The dried polymer is compounded with 0.5 phr of t-butyl peroxide free radical catalyst and subjected to a temperature of 100.degree. C. for 60 minutes. The resulting polymer is a nodular branched copolymer soluble in lubricating oils.

Although the invention is described with reference to particular means, materials, and processes, the invention is not limited except by the scope of the claims.