Title: ETHYLENE α-OLEFTN BLOCK COPOLYMERS AND

METHODS FOR PRODUCTION THEREOF

Technical Field

This invention relates to block polymers containing both crystalline and elastomeric blocks. The copolymers have blocks of polyethylene optionally containing an α-olefin and a non-conjugated diene and blocks containing ethylene and an α-olefin. A novel process for producing the block copolymers is also provided.

BACKGROUND

Block copolymers are well known. They have been used commercially as components in adhesives, as melt processable rubbers, in impact resistant thermoplastics, as compatibilizers, as "surfactants" for emulsifying polymer-polymer blends, and as viscosity index improvers in lubricating oils. A block copolymer is created when two or more polymer molecules of different chemical composition are covalently bonded in an end-to-end fashion. While a wide variety of block copolymer architectures are possible, most block copolymers of interest involve the covalent bonding of hard plastic blocks, which are substantially crystalline or glassy, to elastomeric blocks forming thermoplastic elastomers. Other block copolymers, such as rubber-rubber (elastomer-elastomer), glass-glass, and glass-crystalline block copolymers are also possible and may have commercial importance. Two common types of block copolymer structures are the diblock and tri-block forms. However, multi-block copolymers, in which more than three blocks are bonded together, are also desirable. The multi-block copolymers include either linear multi-block or multi-arm star block polymers.

Tri-block and multi-block copolymers containing "hard" and "soft" blocks have

the unique ability of behaving as thermoplastic elastomers, combining thermoplasticity with rubber-like behavior. The typical requirement for achieving thermoplastic elastomeric behavior is the ability to develop a two-phase physical network. Such a system is composed of a portion of hard block, having a glass transition temperature (T _g ) or melting temperature (T _m ) above the service temperature of a fabricated end use product, and a portion of a soft block, having a T _g below the service temperature. The hard blocks associate to form domains that serve as physical crosslinks and reinforcement sites. The reinforcement sites and physical cross-links are thermally reversible, making it possible to process the polymer as a melt phase material at temperatures above the T _g or T _m of the hard block. Among the advantages of having a physically cross-linked system that is thermally reversible is that while below the T„ or T _m of the hard block such polymers exhibit properties approaching those of fully-cured, i.e. chemically crosslinked elastomers, but unlike such cured elastomers, by heating these polymers above T _g or T _m of the hard block, the physical crosslinks are eliminated and the material can be processed. The advantage of such systems will be well known to those of ordinary skill in the art.

A substantial amount of work has been done in an attempt to synthesize olefinic block copolymers. The ideal catalyst system would produce a "living polymer". Unlike typical Ziegler-Natta polymerization processes, living polymerization processes involve only initiation and propagation steps and essentially lack chain terminating side reactions. This permits the synthesis of the predetermined and well-controlled structures desired in a block copolymer. A polymer created in a "living" system can have a narrow or extremely narrow distribution of molecular weight and be essentially monodisperse. Living catalyst systems are characterized by an initiation rate which is on the order of or exceeds the propagation rate, and the absence of termination or transfer reactions. In addition, these catalyst systems are preferably characterized by the presence of a single type of active site. To produce a high yield of block copolymer product in a polymerization process the catalyst must exhibit living characteristics to a substantial extent.

Anionic polymerization routes to ideal block copolymers have been studied.

Butadiene-isoprene block copolymers have been synthesized using the sequential monomer addition technique. In sequential addition, a certain amount of one of the monomers is contacted with the catalyst. Once a first such monomer has reacted to substantial extinction forming the first block, a certain amount of the second monomer or

monomer species is introduced and allowed to react to form the second block. The process may be repeated using the same or other anionically polymerizable monomers. Ethylene and other α-olefins, such as propylene and butene, are not directly block polymerizable by anionic techniques.

U.S. patent 4,804,794 to Ver Strate, et al., discloses segmented copolymers of ethylene and at least one other alpha-olefin. The copolymers have a narrow MWD

(Mw/ n) less than 2. The copolymers have one segment that is crystallizable and at least one low crystallinity segment. A vanadium catalyst is utilized with an organoaluminum cocatalyst. The polymerization is carried out in a mix-free reactor.

WO 9112-285-A to Turner, et al., discloses a process for production of block copolymers of ethylene with an alpha-olefin and the polymer produced by the process. The process includes sequentially contacting ethylene with an alpha-olefin in the presence of an ionic catalyst to produce a block copolymer. The ionic catalyst comprises the reaction product of a first component which is a bis (cyclopentadienyl) derivative of a metal of Group IN-B of the Periodic Table of the Elements which metal is capable of forming a cation formally having a coordination number of 3 and a valence of -4; and at least one second component comprising a cation capable of donating a proton and a compatible non coordinating anion.

While many patents and publications claim the Ziegler-Νatta catalyzed synthesis of block copolymers from ethylene and propylene, there is little evidence that these products were obtained in high purity. In Boor, J. Ziegler-Νatta Catalysts and Polymerization. Academic Press, 1979, Boor states that the known kinetic features of heterogeneous Ziegler-Νatta catalysts suggest that it is unlikely that block polymers were synthesized in a substantial yield, as compared to the total polymer formed. This publication is incorporated herein by reference for purposes of U.S. patent practice.

In this context, several difficulties arise in the use of known coordination catalysts for the block copolymerization of α-olefins. Among those are the fact that conventional catalysts are typically multi-sited, and a significant fraction of the active sites are unstable. This leads to non-uniform chain initiation and termination which, in turn, lowers the theoretical block copolymer yield. In addition, chain transfer rates during polymerization with known coordination catalysts are high. This is especially true with metallocene catalyst systems where thousands of chains may be produced per active

site.

SUMMARY

The present invention is directed to procedures to make the use of certain coordination catalysts possible for production of alpha-olefin block copolymers of the crystalline-elastomeric type in high purity. These block copolymers and methods of their manufacture by a Ziegler-Natta type catalyst are objects of our invention. We will demonstrate the existence of high yields of true block copolymers. Evidence of the existence of such high yield of true block copolymer, as stated above, has been substantially absent prior to the present invention.

The present invention comprises a novel block polymer having an A block and a B block, and if a diene is present in the A block, a nodular polymer formed by coupling two or more block polymers. The A block is an ethylene polymer optionally containing an alpha-olefin and /or a non-conjugated diene. The diene, if present in the A block, is present in an amount up to 10 mole percent based on the total moles of the monomers of the block copolymer. The B block has a first polymer segment that is an ethylene and an alpha-olefin copolymer segment, the first polymer segment is contiguous to a junction of the A block and the B block. The B block may have a tip segment, the tip segment is furthest from the A B junction, and the tip segment is a polymer of ethylene and an alpha-olefin. The tip segment of the B block may comprise an ethylene, alpha-olefin copolymer with an average ethylene content of at least 60 mole percent based on the total tip segment, the tip segment melts in the range of from 35° C to 130° C as measured by DSC .

The present invention also comprises a process for producing these block copolymers, which has the steps of:

(a) Forming a catalyst species by premixing a vanadium compound and an organoaluminum compound. The pre-mixing step is carried out for a sufficient period of time to provide an adequate amount of active catalyst species;

(b) Feeding the reaction product of step (a) to a mix free reactor concurrently with a monomer stream made up of ethylene, optionally an alpha-olefin and optionally a non-conjugated diene;

(c) Feeding at least a second monomer blend made up of ethylene, and an alpha- olefin;

If a diene is present, the block copolymer may be coupled using the residual olefinic functionality of the diene to produce nodular polymers. Coupling can take place either in the reactor, or post reactor.

The coupled polymer will generally be useful in, among other applications, lubricating oils, as viscosity improvers or dispersants. A coupling agent may be used to couple two or more block copolymers.

These block copolymers find use as thermoplastic elastomers (TPE), plastics blending components, in fuel lubricating and heating oils, as a bitumen modifier, in roof sheeting compounds, and in hot melt adhesives.

These and other features, aspects and advantages of the present invention will become better understood with reference to the following description, appended claims and accompanying drawings where: BRIEF DESCRIPTION OF THE DRAWINGS

Figure 1 is a Differential Scanning Calorimeter (DSC) thermogram for polymer 2A described in Example 2.

Figure 2 is a DSC thermogram for polymer 2B described in Example 2.

Figure 3 is a DSC thermogram of a pure polyethylene A block.

Figure 4 is a schematic representation of a process for producing polymer in accordance with our invention.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The present invention is directed to procedures to make and use certain alpha- olefin block copolymers of the crystalline-elastomeric type in high purity using certain

coordination catalysts. These block copolymers and methods of their manufacture by a Ziegler-Natta type catalyst are among the objects of our invention.

The present invention comprises a novel block copolymer having an A block and a B block and when a diene is present in the A block, a nodular polymer formed by coupling two or more block copolymers. The nodular polymer may optionally contain a coupling agent Y;

(1) "A" denotes a block comprising polyethylene, and optionally an α-olefin comonomer not exceeding 5 mole percent based on the total moles of monomers in the A block, and further optionally containing up to 10 mole percent of a non- conjugated diene. The diene is present at this mole percent based on the total A B block copolymer.

The A block is present in the block copolymer preferably in the range of from 5 to 90 weight percent based on the total weight of the block copolymer. More preferably in the range of from 10 to 60 weight percent, most preferably in the range of from 20 to 50 weight percent.

(2) "B" denotes a block comprising ethylene and an α-olefin copolymer. The B block comprises one or more segments. If there is one segment in the B block, it will be an ethylene, α-olefin segment. If there are two or more segments in the B block, the first segment immediately following the junction of the A and B blocks will be an ethylene α-olefin copolymer segment. The tip or end segment will be located in the portion of the B block furthest from the A B junction. If there are two segments, the second or tip segment will be an ethylene, α-olefin copolymer with an average ethylene content of at least 60 mole percent based on the total moles of the monomers of the tip segment, and which melts in the range of 35 to 130°C, as measured by DSC.

Optionally the B block has an intramolecular composition distribution such that at least two portions of the B block, each portion comprising at least 5 weight percent of the B block, differ in composition by at least 5 weight percent ethylene. The B block is present in the block copolymer in the range of from 10 to 95 weight percent based on the total weight of the block copolymer.

The tip of the B block can comprise up to 50 weight percent of the B block, preferably in the range of from 3 to 20 weight percent, more preferably in the range of from 5 to 15 weight percent, all weight percents of the tip based on the total weight of the B block. The tip segment, when present, is typically the segment furthest from the A B junction.

Y is a coupling agent which has reacted with the residual olefinic functionality in the block polymers and has coupled two or more block polymer molecules.

A is a crystalline block and B has elastomeric segments. B may optionally contain a low level of crystallinity.

COPOLYMER BLOCKS

BLOCK A

Block A comprises polyethylene which optionally may contain up to 10 mole percent of a non-conjugated diene (based on the total moles of the monomers of the A B copolymer). The A block may optionally contain an α-olefin comonomer at a level not exceeding 5 mole percent based on the total moles of the monomers of the A block. If block A contains a non-conjugated diene it will be present in the A block preferably in the range of from 0.01 to 5 mole percent, more preferably in the range of from 0.03 to 2 mole percent, most preferably in the range of from 0.05 to 1 mole percent based on the total moles of the monomers of the A B block copolymer. Block A comprises 5 to 90 weight percent of the entire polymer, preferably 10 to 60 weight percent , most preferably 20 to 50 weight percent of the entire polymer. The A block has a T _m of at least 110° C, preferably at least 105° C, more preferable at least 120° C.

BLOCK B

Block B is an elastomer that comprises an ethylene and an α-olefin copolymer. Block B optionally has an intramolecular-compositional distribution such that at least two portions of the B block, each of said portions comprising at least 5 weight percent of said B block, differ in composition by at least 5 weight percent ethylene. Intramolecular-compositional distribution is the compositional variation, in terms of ethylene, along the polymer chain or block. It is expressed as the minimum difference in

average ethylene composition in weight percent of ethylene that exists between two portions of a single block, each portion comprising at least 5 weight percent of the block. Intramolecular-compositional distribution is determined using the procedures disclosed in U.S. Patent No. 4,959,436, the teachings of which are hereby incorporated by reference for purposes of U.S. patent practice.

The B block comprises 95 to 10 weight percent of the total weight of the block copolymer, preferably 90 to 40 weight percent; more preferably 80 to 50 weight percent.

The B block comprises one or more segments. If there are two or more segments in the B block, the tip or end segment furthest from the junction of the A block and the B block will comprise an ethylene, α-olefin copolymer with an average ethylene content of at least 60 mole percent based on the total moles of the monomers of the tip segment. The tip segment melts in the range of from 35° C to 130° C as measured by DSC

The tip of the B block can comprise up to 50 weight percent of the B block, preferably in the range of from 3 to 20 weight percent, more preferably in the range of from 5 to 15 weight percent, aH weight percents of the tip based on the total weight of the B block. The tip segment, when present, is typically the segment furthest from the A

B junction.

The B block can comprise an average ethylene content in the range of from 20 to 90 mole percent, preferably in the range of from 30 to 85 mole percent, and most preferably in the range of from 50 to 80 mole percent based on the total moles of the monomers of the B block.

The block copolymers of the invention are further characterized in that they have a number average molecular weight of between 750 and 20,000,000 and have a molecular weight distribution characterized by a M _w /M _n ratio of less than 2.5. The block copolymers have an n-hexane soluble portion, at 22 °C not exceeding 50 weight percent, preferably not exceeding 40 weight percent, and more preferably not exceeding 30 weight percent, based on the total weight of the block copolymer. The products of the present invention are further characterized by a relatively small amount of polymer chains in the final product that contain only an A block or only a B block. The presence of such materials could detract from overall product properties. A typical characteristic

of the preferred product of this invention is that the block copolymer contains at least 50 % (weight) of the desired A B structure as polymerized. Product purification is not necessary to obtain good properties.

Monomers

Alpha-olefins particularly useful in the practice of this invention are those having from 3 to 8 carbon atoms, e.g. propylene, butene-1, pentene-1, etc. Alpha-olefins of 3 to 6 carbon atoms are preferred due to economic considerations. The most preferred α- olefin is propylene.

Typical non-limiting examples of non-conjugated dienes useful in the practice of this invention are:

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

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

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

(d) multi-ring fixed and fused ring dienes such as: tetrahydroindene; methyltetra- hydroindene; dicyclopentadiene; bicyclo-(2,2,l)-hepta-2,5-diene; alkenyl, alkylidene, cycloalkenyl and cycloalkylidene norbornenes such as 5-methylene-2- norbornene (MNB), 5-ethylidene-2-norbornene (ENB), 5-propenyl-2- norbornene, 5-(4-cyclopentenyl)-2-norbornene, 5-cyclohexylidene-2-norbomene, vinyl norbornene, and norbornadiene.

Of the non-conjugated dienes useful in the practice of the invention, dienes containing at least one of the double bonds in a strained ring are preferred. The most preferred dienes are 5-ethylidene-2-norbornene and vinyl-norbornene. Conjugated dienes are also contemplated.

Polymerization

The novel polymers of our invention are prepared by polymerization in a mix-free reactor similar to that taught in U.S. Patent No. 4,959,436, the teachings of which were previously incorporated by reference for the purposes of U.S. patent practice.

Previously, those of skill in the art thought that a solution polymerization process such as that taught in U.S. Patent No. 4,959,436 would not be suitable for producing block copolymers such as the ones described above in which one of the blocks, polyethylene, is insoluble in the solvent. The insolubility could lead to reactor fouling and mass transport problems. In turn, these problems could prevent the formation of the desired well-defined polymer structure and significantly reduce catalyst efficiency.

Surprisingly, we have found that the block polymers of our invention can be made in a mix-free reactor when the initial monomer feed consists essentially of ethylene, and optionally such that up to 5 mole percent of the A block is alpha-olefin and optionally a diene sufficient to incorporate up to 10 mole percent of a non-conjugated diene (based on the total of the monomers of the block copolymer). This, the A block, is polymerized first. During this part of the reaction, the polyethylene (A) block may be only partially soluble in the reaction diluent and the insoluble polymer block forms a suspension in the diluent.

Once the polymerization of the A block is substantially complete, one or more additional monomer feeds are introduced into the reactor containing ethylene, and an α- olefin. The reaction of the comonomer mixtures forms the B block of the block polymer or the first segment of the B block if there is more than one segment. The B block is polymerized onto the polyethylene or A block formed earlier. When this second part of the polymerization occurs, there is a noticeable change in the appearance of the reaction medium. As the chains become solubilized through the addition of the B block, the turbidity of the medium decreases appreciably and the quantity of polymer particles in the diluent is markedly reduced. When a tubular reactor is employed, several monomer feeds along the reactor length may be used to control the composition and amount of the

B block and form the segments of the B block. The final feeds to the reactor may contain a higher ethylene/α-olefin ratio to form a semi-crystalline segment at the tip of the B block., giving the B block a melting point in the range of from 35 to 130° C.

Coupling the Polymers

Block polymers of our invention may incorporate a diene. The residual olefinic functionality in diene containing block polymers can be reacted with coupling agents to produce novel nodular polymers.

Suitable coupling reagents and coupling techniques are described in U.S. Patent 4,882,406 the teachings of which have previously been incorporated by reference for purposes of U.S. patent practice. Coupling can take place either within the polymerization reactor or in a post-polymerization reaction. With the diene in the A block, the polyethylene segment containing the diene is in a central polyethylene nodule with EP block extending outwards.

There are various coupling agents that are capable of reacting with the residual unsaturation in the polymer chains to cause coupling of two or more block polymer molecules.

Coupling may be carried out with cationic catalysts such as Lewis acids. Suitable Lewis acids may be selected from the group consisting of: A1X ₃ , BX ₃ , SnX ₄ , SbX ₅ , AlR _y X ₃ . _y where y is 0 to 1.5 and R is a hydrocarbon radical, BX ₄ , TiX ₄ and mixtures thereof, where X is selected from the group consisting of chlorine, bromine, and iodine. Chlorine is preferred. For Lewis acids that do not interfere with the functioning of the catalyst system used to carry out the polymerization, the Lewis acid can be added directly to the reactor so that chain coupling occurs at the same time as the polymerization. Alternately the coupling agent can be added following the polymerization.

According to yet another embodiment the coupling agent may be a free radical catalyst. The free radical catalyst may be a peroxide selected from the group consisting of: dicumyl peroxide, di-tertiarybutylperoxide, t-butylperbenzoate, l,l-di(t- butylperoxy)-3,3,5-trimethyl cyclohexane, and mixtures thereof. Other free radical catalysts include azo-bisisobutylnitrile, azodicarboxylate, and mixtures thereof. Peroxides can couple non-diene containing portions of the chain and produce a cross- linked network. Care must be taken when they are used as coupling agents.

In yet another embodiment the coupling agent may be selected from the group consisting of sulfur dichloride, disulfenyl halides, borane, dithoalkanes, other sulfur and accelerated sulfur curatives and mixtures thereof, such as mercaptobenzothiozole, tetramethylthiuram disulfide, and butyl zymate. It is apparent that any of the conventional vulcanization systems useful for EPDM may be employed.

Resins and other reagents may also be employed for coupling. For example alkyl phenol formaldehyde mixtures will couple olefins in certain cases with catalysts such as ZnC- ₂ , N-bromosuccinimide or diphenylbromomethane.

Also contemplated as a coupling mechanism is the use of irradiation or electron beams.

For certain non-conjugated dienes, such as norbornadiene, vinyl norbornene, dicyclopentadiene and tetrahydroindene, both double bonds are polymerizable to a greater or lesser extent by the polymerization catalysts of this invention. With dienes of this type chains can become chemically coupled to each other during polymerization by reaction of the remaining double bond in an enchained diene monomer with a growing chain. This process will lead to coupling of chains in the reactor even in the absence of a coupling agent Y.

The efficiency of olefin utilization will determine what level of coupling agent to use in relation to the amount of diene in the block copolymer. The purpose is to couple the diblocks to an extent which yields good mechanical properties but does not raise viscosity or produce gel to the extent that the coupled product is not processable.

The Reaction Solvent

Processes in accordance with the present invention produce copolymers by polymerization of a reaction mixture comprised of catalyst, ethylene and at least one additional α-olefin monomer and optionally diene. Polymerization in the presence of a diluent which has the capability to dissolve a major portion of the final product is preferred. Suitable solvents are described in U.S. patent number 4,882,406 the teachings of which are incorporated by reference for purposes of U.S. patent practice.

Polymerization Reactor

These processes are 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 initiated at different times. Suitable reactors are disclosed in U.S. patents 4,959,436 and 4,882,406 both of which have been incoφorated by reference for the puφoses of U.S. patent practice. Additional reaction considerations are also disclosed in these references.

To obtain the desired A B block polymer, it is necessary to add additional reactants (e.g., at least one of the monomers ethylene, α-olefin or diene) either at some point or points along the length of a tubular reactor, or during the course of polymerization in a batch reactor, or at various points in a train of continuous flow stirred reactors. However, it is also preferred to add essentially all of the catalyst at the inlet of a continuous flow reactor or at the onset of batch reactor operation to meet the requirement that essentially all polymer chains are initiated simultaneously. To make diene containing block polymers, diene is fed at the reactor inlet to incoφorate diene into an A block. Multiple feeds of ethylene and propylene can be used to control the amount and composition of the segments in the B block.

Since the tubular reactor is the preferred reactor system for carrying out processes in accordance with the preferred embodiment, the illustrative descriptions and examples that follow are drawn to that system, but will apply to other reactor systems as will readily occur to those of ordinary skill in the art having the benefit of the present disclosure. However, as would readily occur to those of ordinary skill in the art having the benefit of the present disclosure, more than one reactor could be used, either in parallel, or in series with multiple monomer feeds to vary intramolecular composition.

The Catalyst

The composition of the catalyst used to produce ethylene, α-olefin copolymers has a p embodiment 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 that they do not produce a significant amount of polymer which detracts from the performance of the polymer produced. Such

additional active catalyst species may provide as much as 35% by weight of the total copolymer. Preferably, they should account for 10% by weight or less of by the copolymer. Thus, the essentially one active species should provide for at least 65% by weight of the total copolymer produced, preferably for at least 90% by weight 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. These techniques are shown in Cozewith, C. and Ner Strate, G., "Ethylene-Propylene Copolymers. Reactivity Ratios, Evaluation and Significance", Macromolecules. 4, 482 (1971), which is incoφorated herein by reference for puφoses of U.S patent practice.

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

O (1)

II

VCUOR) ₃ . _x ;

VCl _x (COOR) ₃ . _x ; (2)

where x = 0 to 3 and R = a hydrocarbon radical;

VC1 ₄ ;

O

II

N(AcAc) ₂ ;

V(AcAc) ₃ ;

O

II VCl _x (AcAc) ₃ . _x ; (3)

where AcAc = acetyl acetonate; and where x = 1 or 2; and

VCl ₃ .nB;

where n = 2 to 3 and B = Lewis base capable of making hydrocarbon-soluble complexes with VC1 ₃ , such as tetrahydrofiiran, 2-methyl-tetrahydrofuran and dimethyl pyridine. In Formulas (1) and (2) above, R preferably represents a C _j to C 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. Νon-limiting illustrative examples of formulas (1) and (2) compounds are vanadyl trihalides, alkoxy halides and alkoxides such as VOCl ₃ , VOCl ₂ (OBu) where Bu = butyl, NO(OC ₂ H ₅ ) ₃ , and vanadium dichloro hexanoate. The most preferred vanadium compounds are NC1 ₄ , NOCl ₃ , and VOCl ₂ (OR).

As already noted, the co-catalyst is preferably an organoaluminum compound. In

terms of chemical formulas, these compounds could be as follows:

A1R ₃ Al(OR')R_.

AlR _j X R _j Al-O-AlR-.

AIRRX

A1 ₂ R ₃ X ₃

AlRX _j methyl alumoxane

where R and R' represent hydrocarbon radicals, the same or different, as described above with respect to the vanadium compound formula and X is a halogen selected from the group consisting of bromine, iodine, and chlorine. Chlorine is preferred. The most preferred organoaluminum compound for use with a vanadium catalyst is an aluminum alkyl sesquichloride such as Al ₂ Et ₃ Cl ₃ or Al ₂ (iBu) ₃ Cl ₃ . The catalyst and its effects on the polymerization are disclosed in U.S. patent 4,882,406, previously incoφorated by reference for puφoses of U.S patent practice.

With reference again to processes for making copolymer in accordance with our invention, certain combinations of vanadium and aluminum compounds that can comprise the catalyst system can cause branching and gellation during the polymerization for polymers containing high levels of diene. To prevent this from happening, Lewis bases such as ammonia, tetrahydrofiiran, pyridine, tributylamine, tetrahydrothiophene, tetraalkoxysilane, etc., can be added to the polymerization system using techniques well known to those skilled in the art.

Chain transfer reactions during tubular reactor polymerization in accordance with our invention broadens polymer molecular weight distribution and causes the formation of undesirable blocks such as A-only polymer or B-only polymer rather than the desired A B block copolymers of the present invention. It is desireable to operate at low temperature and in the absence of Hydrogen to avoid transfer reactions. U.S. patent 4,882,406 discloses chain transfer reactions. This U.S. patent has previously been incoφorated by reference.

Molecular weight distribution and percent of block polymer in the final product are also affected by catalyst deactivation during the course of the polymerization which leads to termination of growing chains. Early chain termination will reduce the yield of the desired block copolymers. Deactivation can be reduced by using the shortest residence time and lowest temperature in the reactor that will produce the desired

monomer conversions.

Gel Permeation Chromatography (GPC) and several analytical techniques are used to characterize the polymer and its performance in various applications. These techniques have been described in several publications notably U.S. Patent No. 4,989,436 which has been previously incoφorated for puφoses of U.S. patent practice. Molecular weight and composition measurements are described in G. Ver Strate, C. Cozewith, S. Ju, Macromolecules. 21, 3360 (1988). The variety of other techniques used are soundly based in polymer structure characterization as described in "Structure Characterization" The Science and Technology of Elastomers. F. Eirich, editor, Academic Press 1978 Chapter 3 by G. Ver Strate. Differential scanning calorimetry (DSC) is used to characterize the block polymers described herein. The standard protocol for these analysis is to load the calorimeter at 20° C with a specimen free of molding strains, to cool the sample to -75° C, scan to 180° C at 10° C/min., cool to -75° C, and re-run the scan. T _p T _m and heat of fusion are evaluated. In some cases, low melting crystallinity will not be seen on the second scan as it may take many hours to develop even at low temperatures.

Catalyst Preparation

Polymerizations in accordance with the preferred embodiments 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 in U.S. patent 4,959,436, previously incoφorated by reference for puφoses of U. S. patent practice.

Reaction Temperature

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 the reaction mixture spends at high temperature must be short enough to minimize the amount of undesirable chain transfer and catalyst deactivation reactions. Control of the reaction temperature in light of the fact that the reaction is exothermic, is disclosed in U.S. patent 4,959,436 which has been incoφorated by reference for puφoses of U.S. patent practice.

Residence Time

Residence time of the reaction mixture in the mix-free reactor can vary over a wide range. The minimum could be as low as 0.5 seconds. A preferred minimum is 2 seconds. The maximum could be as high as 3600 seconds. A preferred maximum is 900 seconds. The most preferred maximum is 300 seconds.

Process Flow

When a tubular reactor is used 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 promotes homogeneous temperature and polymerization rate at all points in a reactor cross section. Radial temperature gradients may tend to broaden the molecular weight distribution of the copolymer since the polymerization rate is faster in the high temperature regions. Those of ordinary skill in the art 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 Coφoration).

For puφoses of illustration, we assume that a block copolymer of polyethylene and of ethylene and propylene (EP) copolymer is to be produced using as catalyst components vanadium tetrachloride and ethyl aluminum sesquichloride. The polymerization is adiabatic, using hexane diluent for both the catalyst system and the reaction mixture.

In a preferred embodiment, with reference to the process flow diagram in Figure 4, 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 at the temperature set by the temperature bath. The temperature of the bath is set to give the desired 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, where it is intimately mixed with a stream containing hexane diluent and the monomer to be incoφorated into the A block, in this case ethylene, and which is fed through conduit 10. Any suitable mixing device can be used such as 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 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. Stream 10, the hexane with dissolved monomers, may be cooled upstream of mixing zone 9 to provide the desired feed temperature at the reactor inlet.

Tubular reactor 12 is shown with intermediate feed points 13, 14, and 14a where additional monomers (e.g., ethylene and propylene) and/or hexane can be fed to the reactor. The additional feeds are used to control the composition of the block copolymer. The number of side feeds required and the spacing along the reactor length depends on final polymer structure desired. While the reactor can be operated adiabatically, external cooling means such as a cooling jacket surrounding at least a portion of the reactor system 12, can be provided to maintain reaction mixture temperature within desired limits.

Having thus described the above illustrative reactor system, it will readily occur to those of ordinary skill in the art 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.

Functionalization of the Block Copolymers

The polymers produced in accordance with the present invention can be functionalized, i.e., chemically modified, to have at least one functional group present within its structure, which functional group is capable of: (1) undergoing further chemical reaction (e.g. derivatization) with other material/or (2) imparting desirable properties not otherwise possessed by the polymer alone, absent chemical modification. The functional group can be incoφorated into the backbone of the polymer or can be attached as a pendant group from the polymer backbone. The functional group typically

will be polar and contain hetero atoms such as P, O, S, N, halogen and/or boron. It can be attached to the saturated hydrocarbon part of the polymer via substitution reactions or to an olefinic portion via addition or cycloaddition reactions. Alternatively, the functional group can be incoφorated into the polymer by oxidation or cleavage of a small portion of the diene containing portion of the polymer (e.g., as in ozonolysis). Useful functionalization reactions include: maleation, halogenation, "ene" reactions, reactions with a phenol group, reaction at the point of unsaturation with carbon monoxide, reaction by free radical addition or abstraction and reaction by epoxidation or chloroamination.

As indicated, a functionalized polymer is one which is chemically modified primarily to enhance its ability to participate in a wider variety of chemical reactions than would otherwise be possible with the unfunctionalized polymer. In contrast, a derivatized polymer is one which has been chemically modified to perform one or more functions in a significantly improved way relative to the unfunctionalized polymer and/or the functionalized polymer. Representative of such functions are dispersancy and/or viscosity modification in lubricating oil compositions. The derivatized polymers can include the reaction product of the above recited functionalized polymer with a nucleophilic reactant, which includes amines, alcohols, amino-alcohols and mixtures thereof, to form oil soluble salts, amides, imides, oxazolines, reactive metal compounds and esters of mono- and dicarboxylic acids, and anhydrides. Suitable properties sought to be imparted to the derivatized polymer include especially dispersancy, but also multifunctional viscosity modification, antioxidancy, friction modification, antiwear, antirust, anti-seal swell, and the like.

Ash-producing detergents can be made using the functionalized polymers of the present invention as exemplified by oil-soluble neutral and basic salts of alkali or alkaline earth metals with alkyl phenols, alkyl sulfonic acids, carboxylic acids, or organic phosphorus acids characterized by at least one direct carbon-to-phosphorus linkage such as those prepared from the functionalized olefin polymer of the present invention with a phosphorizing agent such as phosphorus trichloride, phosphorus heptasulfide, phosphorus pentasulfide, and sulfur, white phosphorus and a sulfur halide, or phosphorothiotic chloride. Preferred ash-producing detergents which can be derived from the functionalized polymers of the present invention include the metal salts of alkyl sulfonic acids, alkyl phenols, sulfurized alkyl salicylates, alkyl naphthenates and other oil soluble mono- and dicarboxylic acids.

- 21 -

The derivatized polymer compositions of the present invention, can be used as ashless dispersants in lubricant and fuel compositions. Various types of ashless dispersants can be made by derivatizing the polymer of the present invention and are suitable for use in the lubricant compositions. The following are illustrative:

1. Reaction products of functionalized polymer of the present invention derivatized with nucleophilic reagents such as amine compounds, e.g. nitrogen containing compounds, organic hydroxy compounds such as phenols and alcohols.

2. Reaction products of the polymer of the present invention functionalized with an aromatic hydroxy group and derivatized with aldehydes (especially formaldehyde) and amines especially polyalkylene polyamines, through the Mannich reaction, which may be characterized as "Mannich dispersants".

3. Reaction products of the polymer of the present invention which have been functionalized by reaction with halogen and then derivatized by reaction with amines (e.g. direct amination), preferably polyalkylene polyamines.

The functionalized polymers, particularly acid functionalized polymers, of the present invention can be reacted with alcohols, e.g., to form esters. Procedures are well known for reacting high molecular weight carboxylic acids with alcohols to produce acidic esters and neutral esters. These same techniques are applicable to preparing esters from the functionalized polymer of this invention and the alcohols described above. The hydroxy aromatic functionalized polymer aldehyde/amino condensates useful as ashless dispersants in the compositions of this invention include those generally referred to as Mannich condensates. A useful group of Mannich Base ashless dispersants are those formed by condensing phenol functionalized polymer with formaldehyde and polyethylene amines, e.g., tetraethylene pentamine, pentaethylene hexamine, polyoxyethylene and polyoxpropylene amines, e.g., polyoxyproylene diamine and combinations thereof.

A useful class of nitrogen containing condensation products for use in the present invention are those made by a "2-step process" as disclosed in U.S. Patent No. 4,273,891. Condensates made from sulfur-containing condensates are described in U.S.

Patent Nos. 3,368,972; 3,649,229; 3,600,372; 3,649,659; and 3,741,896 These patents

also disclose sulfur-containing Mannich condensates. Useful reactive metals or reactive metal compounds are those which will form metal salts or metal-containing complexes with the functionalized polymer.

The polymer of the present invention may be used as a component of a synthetic base oil. The functionalized polymer, in addition to acting as intermediates for dispersant manufacture, can be used as a molding release agent, molding agent, metal working lubricant, thickeners and the like. The additives of the present invention are primarily useful in lubrication oil compositions which employ a base oil in which the additives are dissolved or dispersed therein. Such base oils may be natural or synthetic. Base oils suitable for use in preparing the lubrication oil composition of the present invention include those conventionally employed as crankcase lubricating oils for spark-ignited and compression-ignited internal combustion engines, such as automobile and truck engines, marine and railroad diesel engines, and the like.

Lubricating oil formulations containing the additives of the present invention conventionally contain other types of additives that contribute other characteristics that are required in the formulation. Typical of such other additives are detergent/inhibitors, viscosity modifiers, wear inhibitors, oxidation inhibitors, corrosion inhibitors, friction modifiers, foam inhibitors, rust inhibitors, demulsifiers, lube oil flow improvers, and seal swell control agents, etc.

APPLICATIONS

Use in Lubricating Oils

The novel block copolymers of the invention may be used as viscosity modifiers or with suitable functionalization and/or derivatization, as multifunctional viscosity modifiers, and as dispersants, for lubricating oils. This is especially true for block polymers where there is a diene in the A block, and the polymers are in turn coupled to form a nodular polymer. From studies of hydrogenated block polymers of polyisoprene and polybutadiene, those of ordinary skill in the art are aware that such structures lead to good viscosity-temperature behavior (Ver Strate, G., Struglinski, M., "Polymers as Rheology Modifiers," Schulz, D. & Glass, J., ed. ACS Symp. 462, p. 257, 1991). Use of block copolymers are disclosed in U.S. patent 4,959,436, which has been previously incoφorated by reference for puφoses of U.S. patent practice. With further modification

- 25 -

catalyst and co-catalyst were fed into a mixing tee as dilute solutions in hexane at a temperature of 10°C. After mixing, the combined catalyst components flowed through a tube with a residence time of 10 seconds at 10°C before entering the reactor. The monomer feed to the reactor inlet was a solution of ethylene in hexane at 20°C which was mixed with the catalyst stream to start the polymerization. The reactor was operated adiabatically so that temperature increased along its length.

After a residence time of 0.024 minutes, during which the block A (polyethylene) was formed, a feed of ethylene and propylene dissolved in hexane was added via a sidestream injection point to begin polymerization of the B block. Two more ethylene- propylene side feeds were added at residence times of 0.064 and 0.1 minutes to increase the length of the B block. The polymerization was quenched with isopropanol at the end of the reactor. The final reaction temperature was 22°C.

In Examples IA and IB no diene was used and the polymerization was quenched at 0.14 min. The reaction conditions of polymerizations IA and IB are shown in Table 1.

Runs IA and IB

A number of polymerization experiments were carried out at the conditions used in runs IA and IB, but with a polymerization quench injected into the reactor at a residence time of 0.024 min. so that only polyethylene was produced. From the amount of polymer collected in a known period of time, it was determined that close to 100% of the ethylene fed to the reactor in the main flow had reacted to form polyethylene. Thus in Examples 1 A and IB, the rate at which the polyethylene A block is produced is equal to the feed rate of ethylene in the main flow. The rate at which the elastomeric B block is produced can be found by subtracting the A block production rate from the measured total polymerization rate. The percentages of A and B block in the polymer are then calculated by dividing the respective polymerization rates of these blocks by the total polymerization rate. The average ethylene content of the polymer is equal to the ethylene content of the A block, which is 100%, times the fraction of the A block in the polymer, plus the ethylene content of the B block times the fraction of B block in the polymer. Thus the ethylene content of the B block can be calculated from the measured average ethylene content of the whole polymer and the polymerization rates from the equation:

- 26 -

Ethylene content of B block, weight percent = (average polymer % ethylene content - 100 x weight fraction of A block in the total polymer)/weight fraction of B block in the total polymer (all terms are in weight units)

The ethylene content of the entire polymer was determined by infrared spectroscopy using the calibration described in I. J. Gardner, C. Cozewith, and G. Ver Strate, Rubber Chemistry and Technology, vol. 44, 1015, 1971.

The calculated polymer composition is shown in Table 2 along with other measurements of the polymer structure (GPC and DSC). Of particular note is the narrow MWD of the polymers.

Tensile properties of the polymers produced were determined in the following manner. A sheet of polymer 15x15x0.2 cm was prepared by compression molding for 15 minutes at 150°C. An aluminum mold was used with Teflon® coated aluminum foil used as a release agent. Dumbbell-type specimens were die cut from the sheet. These specimens in turn were strained in tension at a crosshead speed of 12.5 cm/min. Initial jaw separation was 5 cm. with 3.3 cm of the specimen undergoing most of the deformation between the fiducial marks. Data were collected at 20°C. Engineering modulii were calculated as force at a given percent elongation divided by the original unstrained specimen cross-sectional area.

Table 3 shows the modulii and tensile strength of the polymer for runs IA and IB. The mechanical properties are a function of molecular weight and the polyethylene block content. The modulus of the polymer containing the larger amount of PE block (IA) are slightly higher than that with a somewhat lower polyethylene block content (IB).

Example 2

A second series of polymerization runs were conducted following the procedures outlined in Example 1. The initial monomer feed to the reactor contained only ethylene to produce the polyethylene A block, two side stream feeds were then added to make the B block. A final feed was introduced with a high ethylene content to produce a semi- crystalline EP segment at the end or tip of the B block. Reaction conditions for runs 2 A and 2B are shown in Table 1. In example 2 A a higher initial ethylene feed rate was used

catalyst and co-catalyst were fed into a mixing tee as dilute solutions in hexane at a temperature of 10°C. After mixing, the combined catalyst components flowed through a tube with a residence time of 10 seconds at 10°C before entering the reactor. The monomer feed to the reactor inlet was a solution of ethylene in hexane at 20°C which was mixed with the catalyst stream to start the polymerization. The reactor was operated adiabatically so that temperature increased along its length.

After a residence time of 0.024 minutes, during which the block A (polyethylene) was formed, a feed of ethylene and propylene dissolved in hexane was added via a sidestream injection point to begin polymerization of the B block. Two more ethylene- propylene side feeds were added at residence times of 0.064 and 0.1 minutes to increase the length of the B block. The polymerization was quenched with isopropanol at the end of the reactor. The final reaction temperature was 22°C.

In Examples IA and IB no diene was used and the polymerization was quenched at 0.14 min. The reaction conditions of polymerizations IA and IB are shown in Table 1.

Runs IA and IB

A number of polymerization experiments were carried out at the conditions used in runs IA and IB, but with a polymerization quench injected into the reactor at a residence time of 0.024 min. so that only polyethylene was produced. From the amount of polymer collected in a known period of time, it was determined that close to 100% of the ethylene fed to the reactor in the main flow had reacted to form polyethylene. Thus in Examples 1 A and IB, the rate at which the polyethylene A block is produced is equal to the feed rate of ethylene in the main flow. The rate at which the elastomeric B block is produced can be found by subtracting the A block production rate from the measured total polymerization rate. The percentages of A and B block in the polymer are then calculated by dividing the respective polymerization rates of these blocks by the total polymerization rate. The average ethylene content of the polymer is equal to the ethylene content of the A block, which is 100%, times the fraction of the A block in the polymer, plus the ethylene content of the B block times the fraction of B block in the polymer. Thus the ethylene content of the B block can be calculated from the measured average ethylene content of the whole polymer and the polymerization rates from the equation:

Ethylene content of B block, weight percent = (average polymer % ethylene content - 100 x weight fraction of A block in the total polymer)/weight fraction of B block in the total polymer (all terms are in weight units)

The ethylene content of the entire polymer was determined by infrared spectroscopy using the calibration described in I. J. Gardner, C. Cozewith, and G. Ver Strate, Rubber Chemistry and Technology, vol. 44, 1015, 1971.

The calculated polymer composition is shown in Table 2 along with other measurements of the polymer structure (GPC and DSC). Of particular note is the narrow MWD of the polymers.

Tensile properties of the polymers produced were determined in the following manner. A sheet of polymer 15x15x0.2 cm was prepared by compression molding for 15 minutes at 150°C. An aluminum mold was used with Teflon® coated aluminum foil used as a release agent. Dumbbell-type specimens were die cut from the sheet. These specimens in turn were strained in tension at a crosshead speed of 12.5 cm/min. Initial jaw separation was 5 cm. with 3.3 cm of the specimen undergoing most of the deformation between the fiducial marks. Data were collected at 20°C. Engineering modulii were calculated as force at a given percent elongation divided by the original unstrained specimen cross-sectional area.

Table 3 shows the modulii and tensile strength of the polymer for runs IA and IB. The mechanical properties are a function of molecular weight and the polyethylene block content. The modulus of the polymer containing the larger amount of PE block (IA) are slightly higher than that with a somewhat lower polyethylene block content (IB).

Example 2

A second series of polymerization runs were conducted following the procedures outlined in Example 1. The initial monomer feed to the reactor contained only ethylene to produce the polyethylene A block, two side stream feeds were then added to make the B block. A final feed was introduced with a high ethylene content to produce a semi- crystalline EP segment at the end or tip of the B block. Reaction conditions for runs 2 A and 2B are shown in Table 1. In example 2 A a higher initial ethylene feed rate was used

than in Example 2B to give the polymer a higher molecular weight and a greater percentage of A block.

These polymers were characterized in a manner similar to the polymers produced in Example 1. The results of these analyses are listed in Table 2. The semicrystalline end segment of the B block of Example 2A averaged 72.2 weight percent ethylene, while the semicrystalline end segment of the B block of Example 2B averaged 70 weight percent ethylene. DSC analysis of the polymers, as shown in Figures 1 and 2, show that the polymers contain a semi-crystalline fraction melting at 42° C in addition to a polyethylene fraction which melts at 122 to 124° C. The modulii and tensile strength of the polymers for runs 2 A and 2B are shown in Table 3.

Example 3

A polymerization was carried out by the procedure in Example 1 using the reaction conditions as shown in Table 4 (samples 3 A and 3B). The diene, ENB, was added to the main reactor feed to produce a polymer containing ENB in the PE block. Ethylene and propylene feeds were added to the reactor at residence times of 0.024 and 0.066 min. ENB feed rates were 2.8 and 1.7 g/hr. and the corresponding polymers contained 0.333 and 0.14 weight percent ENB. These polymers when coupled are useful as lubricating oil viscosity modifiers.

Example 4

In this example, a number of A B block polymers made by the procedure in

Example 1 but over a broad range of reaction conditions, are tested for solubility in hexane at 22°C. The puφose of this testing is to determine how much B block is unconnected to an A block. The composition and molecular weight of the polymers vary widely. Solubility is determined by pressing 2.0 g of the block polymer onto a 20 mesh screen and immersing the polymer and screen in 200 cc of n-hexane. Wide-mouthed bottles were used and were occasionally swirled over a period of 3 to 5 days. The screen is removed and dried to constant weight in a vacuum oven to determine the amount of insoluble polymer. The hexane supernatant liquid is evaporated to dryness and the residue is weighed to measure the amount of soluble polymer. The sum of the two fractions showed 100% of the starting polymer is accounted for.

A control sample of a high density polyethylene which was melt blended with EPDM in a Brabender mixing head at 180°C was also extracted in the same manner. These results are presented in Table 5. In the control blend, all 40% of the EPDM was extractable, showing that the rubber is soluble, even at high PE block content, if it is not attached to a PE block. An infrared analysis showed the soluble material to be over 98% EPDM. PE is not extracted. All of the block polymers of Table 5 show soluble rubber of less than 25%.

Example 5 (Prophetic Example)

In this example analyses for PE block content and yield of A B block polymer as a percentage of the total product is described. Three A B block copolymers with a diene containing segment in the A block, are produced by the procedure described in Example 1. Nearly 100% of the ethylene has reacted by the time that the first ethylene/propylene side stream feed is added to make the elastomeric B block. Thus, the weight percent of A block in a polymer can be estimated by dividing the ethylene feed rate in the main flow to the reactor inlet by the total polymerization rate. We can also estimate the amount of A block by dividing the heat of fusion measured by DSC over the melting range of 80 °C to 135° C, by the heat of fusion measured by DSC for a pure polyethylene A block of approximately the same molecular weight, as shown in Figure 3, made by adding only an ethylene feed to the reactor. A value of 181 J/g. is used for the heat of fusion of polyethylene based on averaging the results from a number of samples.

The polymer samples are fractionated in a Kumagawa apparatus. In this apparatus an individual sample is sequentially extracted with a series of solvents of increasing boiling point. For each solvent continuous extraction is carried out until all soluble polymer is dissolved. The solvents used and their boiling points (bp) were: n- hexane (bp=69°C), cyclohexane (bp=81°C), n-heptane (bp= 98°C), and toluene (bp= 111°C). The polymer soluble in each solvent is recovered, weighed, and analyzed by DSC. By determining the amount of polymer soluble in each solvent and the amount and percentage of PE block in that soluble portion, the percentage of the portion that was non-crystalline EP block can be calculated.

Although the present invention has been described in considerable detail with reference to certain preferred versions thereof, other versions are possible. Therefore, the spirit and scope of the appended claims should not be limited to the description of the

preferred versions contained herein.

TABLE 1

EXAMPLE IA IB 2A 2B

MAIN FLOW g/h hexane 53803 53803 53803 53803 propylene 0 0 0 0 ethylene 151 124 151 73

ENB 0 0 0 0

VC14 1.8 1.5 2.4 2.4

Al/Vmol/mol 8 8 8 8

SIDE STREAM 1, g/h hexane 8910 8910 8910 8910 propylene 1228 1354 1125 1125 ethylene no 148 122 122

SIDE STREAM 2, g h hexane 6138 6138 5910 5910 propylene 358 509 413 413 ethylene 85 110 130 130

SIDE STREAM 3, g/hr hexane 6217 6217 7920 7920 propylene 347 405 510 510 ethylene 80 108 255 255

TEMPERATURE.'C feed 20 20 19 19 reactor outlet 22 22 25 24

RESIDENCE TIME, min. to side stream 1 0.024 0.024 0.024 0.024 to side stream 2 0.064 0.064 0.109 0.109 to side stream 3 0.10 0.10 0.147 0.147 to side stream 4

Total 0.139 0.139 0.183 0.183

PROCESS RESULTS wt % C2 ⁼ in polymer 71.6 70.8 72.2 70.1 wt % ENB in polymer 0 0 0 0 ooney (l+4, 150 ^β C) 109 91.1 114 131

Mwx lO-3 189 246 222 209 n x lO-3 108 149 115 106

Mw/Mn 1.67 1.7 1.91 1.99

Poly Rate, g/h 387 368 689 597

C2=conv *, % 65 54.8 75.6 72.2

C3=conv », % 5.7 4.4 9.4 8.7

Cat eff,g poly/g VC1 ₄ 215 245.3 297 249 conv = conversion

TABLE 2

TABLE 3

TABLE 4 (Example 3)

*conv = conversion

TABLE 5

Run Wt. %C2= Mnxl0-3 Mwxl0-3 Hexane soluble, inPoly. %

317a 68 75 139 12.1

317b 68 97 193 13.0

317c 71 118 228 4.9

317d 69 92 189 12.5

318a 63 69 118 22.1

318b 62 62 118 23.5

318c 64 88 208 16.6

318d 66 92 179 16.9

319a 66 108 160 13.2

319c 68 108 230 7.8

320a 71 108 206 4.1

320c 70 128 237 3.3

323a 72 137 289 2.9

323b 71 152 307 2.2

332a 68 149 258 11.3

333a 68 104 212 7.7

334a 69 126 195 4.9

334b 67 117 178 8.0

335a 66 94 143 10.1

335b 70 - - 6.5

336a 69 - - 15.2

336d 66 - - 19.0

336e 69 74 147 3.7

338b - - - 6.0 %HDPE/ - - - 39.6 %EPDM %HDPE/ - - - 61.0 %EPDM