Constrained geometry catalysts have found wide acceptance in the manufacture of various olefinic polymers, such as the various ethylene, propylene and diene polymers.

These catalysts comprise a metal coordination complex which itself comprises a metal of group 4 of the Periodic Table of the Elements and a delocalized-bonded moiety substituted with a constrain-inducing moiety, the complex having a constrained geometry about the metal atom such that the angle at the metal between the centroid of the delocalized, substituted-bonded moiety and the center of at least one remaining substituent was less than such angle in a similar complex containing a similar s-bonded moiety lacking in such constrain-inducing substituent. The catalyst further comprises a cocatalyst and an activator. "Delocalized-bonded moiety"means an unsaturated organic moiety, such as those comprising ethylenic or acetylenic functionality, in which the- electrons were donated to the metal to form a bond.

The metal atom was the active site of each discreet CGC unit and since each such unit has a single metal atom, these catalysts tend to produce in a highly efficient manner high molecular weight (for example, greater than 10,000 weight average molecular weight) olefin polymers with a narrow MWD (for example, 2 or less) over a wide range of polymerization conditions. CGCs were especially useful for the formation of ethylene homopolymers, copolymers of ethylene and one or more a-olefins (that is, olefins having three or more carbon atoms with the ethylenic unsaturation between the first and second carbon atoms), and interpolymers of ethylene, propylene and a diene monomer (for example, EPDM terpolymers).

While a narrow MWD can impart useful properties to ethylene-based polymers for certain applications, for example, transparency in films, ethylene-based polymers with a broad MWD (for example, greater than 2) usually process more efficiently and have better physical properties, for example, temperature performance, for such applications as injection molded or extruded articles, for example, gaskets and wire and cable coatings, than do ethylene-based polymers with a narrow MWD. Various processes were known for producing broad MWD ethylene-based polymers or polymer blends with a CGC, but all were subject to improvement.

For example, one process for producing such polymers or polymer blends requires the use of multiple reactors deployed in parallel with each reactor containing the same CGC but operated under different polymerization conditions. The product outputs of the reactors were then blended with one another. This produces a polymer blend with a substantially uniform molecular architecture, which was often a desirable property, particularly for elastomers (that is, polymers with a crystallinity of less than 45 percent).

For polymer blends of similar crystallinity, those blends of substantially uniform molecular architecture generally exhibit superior physical performance properties, for example, tensile, modulus, tear, etc., than those blends of a relatively nonuniform molecular architecture."Substantially uniform molecular architecture"means that each polymer molecule of the blend has substantially the same comonomer content and distribution although the polymer molecules from one reactor differ in weight average molecular weight (Mw) from the polymer molecules produced in the other reactor (s).

One difficulty with this process was that it requires balancing the operation and output of one reactor with the other reactor (s). Another difficulty was that it requires a separate, post-reaction blending step. Yet another difficulty was that with the use of multiple reactors, the ratio of high molecular weight (Mw) to low Mw components in the polymer blend was limited to the capacity of each reactor.

In another process, multiple reactors were deployed in series with each reactor operated at substantially the same polymerization conditions but with each reactor containing a different CGC. The output of the first reactor becomes, of course, a feed for the second reactor, and the product output of the second reactor was a polymer blend.

While this process avoids the need for a post-reaction blending step, it still requires balancing the operation of one reactor with the other reactor (s) in the series, and the

output of the process was limited by the capacity of the reactors. Moreover, this process often produces a blend in which the molecular architecture was not uniform.

Variations on both of these multiple reactor processes were known, for example, operating the multiple reactors deployed in series at dissimilar conditions, using a catalyst other than or in addition to a CGC, etc., and USP 5,844,045 to Kolthammer and Cardwell, provides a representative description of a multiple reactor process. However, producing a polymer blend in a single reactor, that is, a reactor blend, saves all the costs associated with running multiple reactors. Moreover, the ratio of high molecular weight (Mw) to low Mw components in the polymer blend can be controlled by controlling the weight ratio of one catalyst to another, and thus the capacity of the individual reactors was not a constraining consideration with respect to this property.

For example, USP 4,937,299 to Ewen and Welborn teaches a process for producing (co) polyolefin reactor blends comprising polyethylene and copolyethylene-a- olefins. These blends were prepared in a single reactor by simultaneously polymerizing ethylene and copolymerizing ethylene and an a-olefin in the presence of at least two different metallocenes and an alumoxane. However, Ewen and Welborn do not teach (i) the use of mixed CGC catalyst systems, or (ii) producing an ethylene-based polymer blend having an MWD (a) of at least 2, and (b) at least ten percent greater than either ethylene- based polymer component of the blend prepared in a single reactor with any single component of the mixed catalyst system under similar polymerization conditions. Ewen and Welborn also do not teach the production of an ethylene-based polymer blend in which each polymer component of the blend has a uniform molecular architecture (at least with respect to the polymer units derived from ethylene and the a-olefin).

USP 5,359,015 to Jejelowo teaches a process of producing polyolefins having a controllable broaden MWD utilizing transition metal metallocene catalyst systems comprising a first component comprising at least one transition metal metallocene having at least one cyclopentadienyl ring that was substituted with a first substituent having a secondary or tertiary carbon atom through which it was covalently bonded to the at least on cyclopentadienyl ring in the system, a second component comprising at least one transition metal metallocene having at least one cyclopentadienyl ring that was substituted with a second substituent that was hydrogen or optionally a second hydrocarbon substituent different from the first substituent, and an activator selected from ionic activators or alumoxane or a combination of the two. The MWD of the polymer produced

by the catalyst system was generally somewhere between the high and low MWD that such catalyst system components would produce if utilized alone.

USP 5,627,117 to Mukaiyama and Oouchi teaches a process for producing a polyolefin with a wide MWD, the process employing an olefin polymerization catalyst comprising a transition metal compound having at least two transition metals in which at least one of the metals was bonded to a ligand having a cyclopentadienyl skeleton at least one of the metals was Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W and lanthanoid metals and the other was a selected transition metal.

WO 93/13143 to Parikh, Cardwell and Kolthammer teaches a process of producing an interpolymer product comprising a first homogeneous ethylene/a-olefin interpolymer and at least one-second ethylene/a-olefin interpolymer. The process comprises the step of using at least two CGCs having different reactivities such that the first ethylene/a-olefin interpolymer has a narrow MWD with a very high comonomer content and a high molecular weight and the second ethylene/a-olefin interpolymer also has a narrow MWD but a low comonomer content and a molecular weight lower than that of the first interpolymer. The first and second ethylene/a-olefin interpolymers can be polymerized in a single reactor.

WO 99/31147 to Nemzek, Karol and Kao teaches a gas phase ethylene polymerization process which uses a mixed catalyst system comprising at least one supported and at least one unsupported metallocene catalyst. The metallocene catalysts include CGCs, the polymerization process can be conducted in a single reaction vessel, and the process produces a polymer blend. However, none of the polymer blends reported in the examples have an MWD greater than any of the polymer components of the blend, and the molecular architecture of the blend polymer components was unreported.

None of these references, the U. S. patents teach the use of a mixed CGC system to produce a reactor blend (i) having an MWD (a) of at least 2, and (b) at least ten percent greater than either ethylene-based polymer component of the blend prepared in a single reactor with any single component of the mixed catalyst system under similar polymerization conditions, and (ii) in which each polymer component of the blend has a uniform molecular architecture (at least with respect to the polymer units derived from ethylene and the a-olefin).

According to one embodiment of this invention, an ethylene-based polymer blend (i) having an MWD (a) of at least 2, and (b) at least ten percent greater than any ethylene- based polymer component of the blend prepared in a single reactor with any single component of the mixed catalyst system under similar polymerization conditions, and (ii) in which each polymer component of the blend has a uniform molecular architecture (at least with respect to the polymer units derived from ethylene and the a-olefin) was prepared by contacting under polymerization conditions and in a single reaction vessel: A. ethylene, B. at least one C3-C20 a-olefin, and C. a mixed CGC system comprising a first catalyst and a second catalyst, each catalyst having substantially the same reactivity ratio and each catalyst comprising: 1. A metal complex of formula I ZLMXpX'q (I) wherein M was a metal of Group 4 of the Periodic Table of the Elements having an oxidation state of +2, +3 or +4 bound in an T15 bonding mode to L; L was a cyclopentadienyl-, indenyl-, tetrahydroindenyl-, fluorenyl-, tetrahydrofluorenyl-, or octahydrofluorenyl-group covalently substituted with at least the divalent moiety, Z, and L further may be substituted with from 1 to 8 substituents independently selected from the group consisting of hydrocarbyl, halo, halohydrocarbyl, hydrocarbyloxy, dihydrocarbylamine, dihydrocarbylphosphino or silyl groups containing up to 20 nonhydrogen atoms; Z was a divalent moiety, or a moiety comprising one 6-bond and a neutral two electron pair able to form a coordinate-covalent bond to M, Z comprising boron, or a member of Group 14 of the Periodic Table of the Elements, and also comprising nitrogen, phosphorus, sulfur or oxygen; X was an anionic ligand group having up to 60 atoms exclusive of the class of ligands that were cyclic, delocalized, n-bond ligand groups; X'independently each occurrence was a neutral ligating compound having up to 20 atoms; p was 0,1 or 2, and was two less than the formal oxidation state of M, with the proviso that when X was a dianionic ligand group, p was 1; and

q was 0,1 or 2; and 2. An activating cocatalyst; with the provisos that (i) the first catalyst was different from the second catalyst, (ii) the first catalyst has a reactivity ratio that was substantially the same as the reactivity ratio of the second catalyst with respect to ethylene and the at least one C3-C20 a-olefin, and (iii) the weight ratio of the first catalyst to the second catalyst, based on the weight of the metal M in each catalyst, was between 90: 10 and 10: 90.

In another embodiment of the invention, an ethylene-based polymer blend having an MWD (a) of at least 2, and (b) at least ten percent greater than any ethylene-based polymer component of the blend prepared in a single reactor with any single component of the mixed catalyst system under similar polymerization conditions was prepared by contacting under polymerization conditions and in a single reaction vessel: A. ethylene, B. at least one C3-C20 a-olefin, C. at least one polyene, and D. a mixed CGC system comprising a first catalyst and a second catalyst, each catalyst having substantially the same reactivity ratio and each catalyst comprising: 1. A metal complex of formula 1, ZLMXpX'q (I) and 2. an activating cocatalyst; with the provisos that (i) the first catalyst was different from the second catalyst, and (ii) the weight ratio of the first catalyst to the second catalyst, based on the weight of the metal M in each catalyst, was between 90: 10 and 10: 90. The definition of Z, L, M, X, X', p and q were as defined above.

In both embodiments, the polymer blend may be recovered from the reaction vessel in any convenient manner.

Each CGC of the system produces an ethylene/a-olefin polymer that has substantially the same molecular architecture as the ethylene/a-olefin polymer produced by the other CGC of the system, but each polymer has a different molecular weight. The reaction temperature controls the molecular weights of the copolymers. With respect to

ethylene/a-olefin/polyene polymer blends, the molecular architecture of a polymer produced by one CGC of the system may differ from the molecular architecture of a polymer produced by the other CGC of the system because the reactivity ratio of the polyene may be different with each CGC of the system (although the size and distribution of the ethylene runs in each polymer molecule may be substantially similar).

The polymer blend also has a rheology ratio greater than any ethylene-based polymer component of the blend prepared in a single reactor with any single component of the mixed catalyst system under similar polymerization conditions.

By"mixed catalyst system"was meant that each CGC of the system was different from the other CGC. The CGCs can differ in one or more of their respective constituent parts, that is, the metal and/or organic ligand component of the metal complex, the cocatalyst and the activator. The mixed catalyst system can comprise two or more CGCs, but dual systems (that is, systems containing essentially only two CGCs) were preferred.

FIG. I was a flow diagram illustrating a continuous polymerization process for the production of a polymer blend in a single reaction vessel using a mixed catalyst system.

FIG. 2 was a viscosity shear rate curve at 190 C reporting the superior processability of 30 Mooney ethylene/1-octene elastomer blend made with a dual GCG system as compared to elastomers made with only one component of the dual CGC system.

FIG. 3 was Gottfert Rheotens Data at 190 C reporting the superior melt strength of 30 Mooney ethylene/I-octene elastomer blend made with a dual GCG system as compared to an elastomer made with only one component of the dual CGC system.

The blend components of this invention were either homopolymers of ethylene (CH2=CH2) or polymers, that is, interpolymers, of ethylene with at least one C3-C20 a- olefin (preferably an aliphatic (x-olefin) comonomer, and/or a polyene comonomer, for example, a conjugated diene, a nonconjugated diene, a triene, etc. The term interpolymer includes copolymers, for example ethylene/propylene (EP), and terpolymers, for example EPDM, but it was not limited to polymers made with only ethylene and one or two monomers. Examples of the C3-C20 a-olefins include propene, 1-butene, 4-methyl-1- pentene, 1-hexene, 1-octene, I-decene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1- octadecene and 1-eicosene. The a-olefin can also contain a cyclic structure such as

cyclohexane or cyclopentane, resulting in an a-olefin such as 3-cyclohexyl-1-propene (allyl-cyclohexane) and vinyl-cyclohexane. Although not a-olefins in the classical sense of the term, for purposes of this invention certain cyclic olefins, such as norbornene and related olefins, were a-olefins and can be used in place of some or all of the a-olefins described above. Similarly, styrene and its related olefins (for example, a-methylstyrene, etc.) were a-olefins for purposes of this invention.

Polyenes were unsaturated aliphatic or alicyclic compounds containing more than four carbon atoms in a molecular chain and having at least two double and/or triple bonds, for example, conjugated and nonconjugated dienes and trienes. Examples of nonconjugated dienes include aliphatic dienes such as 1,4-pentadiene, 1,4-hexadiene, 1,5- hexadiene, 2-methyl-1,5-hexadiene, 1,6-heptadiene, 6-methyl-1,5-heptadiene, 1,6- octadiene, 1,7-octadiene, 7-methyl-1,6-octadiene, 1,13-tetradecadiene, 1,19-eicosadiene, and the like; cyclic dienes such as 1,4-cyclohexadiene, bicyclo [2.2.1] hept-2,5-diene, 5- <BR> <BR> <BR> <BR> ethylidene-2-norbornene, 5-methylene-2-norbornene, 5-vinyl-2-norbornene, bicyclo [2.2.2] oct-2,5-diene, 4-vinylcyclohex-I-ene, bicyclo 1,7,7- trimethylbicyclo- [22. 1] hept-2,5-diene, dicyclopentadiene, methyltetrahydroindene, 5- allylbicyclo [2.2.1] hept-2-ene, 1,5-cyclooctadiene, and the like; aromatic dienes such as 1,4-diallylbenzene, 4-allyl-I H-indene; and trienes such as 2,3-diisopropenylidiene-5- norbornene, 2-ethylidene-3-isopropylidene-5-norbornene, 2-propenyl-2,5-norbornadiene, 1,3,7-octatriene, 1,4,9-decatriene, and the like; with 5-ethylidene-2-norbornene, 5-vinyl-2- norbornene and 7-methyl-1,6-octadiene preferred nonconjugated dienes.

Examples of conjugated dienes include butadiene, isoprene, 2,3- 3,1- 1,3- pentadiene (CH3CH=CH-CH=CH2; commonly called piperylene), 3-methyl-1,3- pentadiene, 3-ethyl-1,3-pentadiene, and the like; with 1,3- pentadiene a preferred conjugated diene.

Examples of trienes include 1,3,5-hexatriene, 2-methyl-1,3,5-hexatriene, 1,3,6- heptatriene, 1,3,6-cycloheptatriene, 5-methyl-1,3,6-heptatriene, 5-methyl-1,4,6- heptatriene, 1,3,5-octatriene, 1,3,7-octatriene, 1,5,7-octatriene, 1,4,6-octatriene, 5-methyl- 1,5,7-octatriene, 6-methyl-1,5,7-octatriene, 7-methyl-1,5,7-octatriene, 1,4,9-decatriene and 1,5,9-cyclodecatriene.

Polymer blends comprising copolymers of ethylene and one aliphatic C3-C20 a- olefin or one polyene (either conjugated or nonconjugated) can be prepared using the process of this invention. Polymer blends comprising interpolymers of ethylene, at least one aliphatic C3-C20 a-olefin, and/or at least one polyene (either conjugated or nonconjugated) can also be made by using this process. Exemplary copolymers include ethylene/propylene, ethylene/butene, ethylene/I-octene, ethylene/5-ethylidene-2- norbornene, ethylene/5-vinyl-2-norbornene, ethylene/-1,7-octadiene, ethylene/7-methyl- 1,6-octadiene and ethylene/1,3,5-hexatriene. Exemplary terpolymers include ethylene/propylene/1-octene, ethylene/butene/1-octene, ethylene/propylene/5-ethylidene-2- norbornene, ethylene/butene/5-ethylidene-2-norbornene, ethylene/butene/styrene, ethylene/1-octene/5-ethylidene-2-norbornene, ethylene/propylene/1, 3-pentadiene, ethylene/propylene/7-methyl-1,6-octadiene, ethylene/butene/7-methyl-1,6-octadiene, ethylene/1-octene/1,3-pentadiene and ethylene/propylene/1,3,5-hexatriene. Exemplary tetrapolymers include ethylene/propylene/1-octene/diene (for example ENB), ethylene/butene/1-octene/diene and ethylene/propylene/mixed dienes, for example ethylene/propylene/5-ethylidene-2-norbornene/piperylene. In addition, the blend components made using the process of this invention can include minor amounts, for example 0.05-0.5 percent by weight, of long chain branch enhancers, such as 2,5- norbornadiene (aka bicyclo [2,2,1] hepta-2,5-diene), diallylbenzene, 1,7-octadiene (H2C=CH (CH2) 4CH=CH2), and 1,9-decadiene (H2C=CH (CH2) 6CH=CH2).

Typically, the blend components made by the process of this invention comprise at least 20, preferably at least 30 and more preferably at least 40, weight percent ethylene; at least 5, preferably at least 15 and more preferably at least 25, weight percent of at least one a-olefin; and, if a polyene-containing terpolymer, greater than 0, preferably at least 0.1 and more preferably at least 0.5, weight percent of at least one conjugated or nonconjugated polyene. As a general maximum, the blend components made by the process of this invention comprise not more than 95, preferably not more than 85 and more preferably not more than 75, weight percent ethylene; not more than 80, preferably not more than 70 and more preferably not more than 60, weight percent of at least one a- olefin; and, if a terpolymer, not more than 20, preferably not more than 15 and more preferably not more than 12, weight percent of at least one of a conjugated or nonconjugated diene. All weight percentages were based on weight of the blend.

The polydispersity (molecular weight distribution or Mw/Mn or MWD) of the polymer blend generally ranges from at least 2, preferably at least 2.1, and especially at least 2.2 to 10, preferably 6, and especially 4. One hallmark of this invention was that the MWD of the polymer blend was at least 10, preferably at least 15 and more preferably at least 20, percent greater than a polymer blend component prepared in a single reaction vessel with either the first or second catalyst alone under similar polymerization conditions.

The polydispersity index was typically measured by gel permeation chromatography (GPC) on a Waters 150 C high temperature chromatographic unit equipped with three linear mixed bed columns (Polymer Laboratories (10 micron particle size)) operating at a system temperature of 140 C. The solvent was 1,2,4-trichlorobenzene from which 0.5 percent by weight solutions of the samples were prepared for injection. The flow rate was 1.0 milliliter/minute, and the injection size was 100 microliters.

The molecular weight determination was deduced by using narrow molecular weight distribution polystyrene standards (from Polymer Laboratories) in conjunction with their elusion volumes. The equivalent polyethylene molecular weights were determined by using appropriate Mark-Houwink coefficients for polyethylene and polystyrene (as described by Williams and Ward in Journal of Polymer Science, Polymer Letters, Vol. 6, (621) 1968) to derive the equation: (a)(Mpolystyrene)bMpolyethylene= In this equation, a = 0.4316 and b = 1.0. Weight average molecular weight, Mw, was calculated in the usual manner according to the formula: Mw = E (ws) (Mi) where wi and Mi were the weight fraction and molecular weight respectively of the jth fraction eluting from the GPC column. Generally, the Mw of the polymer blend ranges from 10,000, preferably 20,000, more preferably 40,000, and especially 60,000, to 1,000,000, preferably 800,000, more preferably 600,000, and especially 500,000.

The polymer blends made by the process of this invention cover a range of viscosities, depending upon the molecular weight of the blend and optional post-

polymerization rheological modification. In general, the blend viscosity was characterized by a Mooney viscosity which was measured according to ASTM D 1646-89 using a shear rheometer at 125 C. The polymer blend Mooney viscosity generally ranges from a minimum of less than 0.01, preferably 0.1, more preferably 1, and especially 15 to a maximum of 150, preferably 125, more preferably 100, and especially 80.

The rheological or shear thinning behavior of the ethylene interpolymer was determined by measuring the ratio of interpolymer viscosity at 0.1 rad/sec to viscosity at 100 rad/sec. This ratio was known as the Rheology Ratio (RR), V0.1/V100, or more simply, 0.1/100. The RR was an extension of l, o/12 and as such, in those instances in which the measurement of 12 and 110 were difficult, for example, the 12 was less than 0.5, or the molecular weight of the interpolymer was relatively high, or the Mooney viscosity of the interpolymer was greater than 35, the RR of the interpolymer can be measured using a parallel plate rheometer. One hallmark of this invention was that the rheology ratio of the polymer blend was typically greater than that of a polymer blend component of substantially the same Mooney viscosity and prepared in a single reaction vessel with either the first or second catalyst alone under similar polymerization conditions.

The density of the polymer blends was measured according to ASTM D-792, and this density ranges from a minimum of 0.850 grams/cubic centimeter (g/cm3), preferably 0.853 g/cm3, and especially 0.855 g/cm3, to a maximum of 0.970 g/cm3, preferably 0.940 g/cm3, and especially 0.930 g/cm3. For those polymer blends that were elastomers, that is, with a crystallinity less than 45 percent, the maximum density was 0.895, preferably 0.885 and more preferably 0.875, g/cm3.

For polymer blends intended for use as elastomers, the crystallinity was preferably less than 40, more preferably less than 30, percent, preferably in combination with a melting point of less than 115, preferably less than 105, C, respectively. Elastomeric polymer blends with a crystallinity of 0 to 25 percent were even more preferred. The percent crystallinity was determined by dividing the heat of fusion as determined by differential scanning calorimetry (DSC) a of polymer blend sample by the total heat of fusion for that polymer blend sample. The total heat of fusion for high-density homopolymer polyethylene (100 percent crystalline) was 292 joule/gram (J/g).

Mixed Catalyst System The constrained geometry metal complexes of the mixed catalyst system, and methods for their preparation, were disclosed in U. S. S. N. 545,403 filed July 3,1990 (EP- A-416,815); EP-A-514,828; USP 5,721,185 and USP 5,374,696; as well as USP 5,470,993,5,374,696,5,231,106,5,055,438,5,057,475,5,096,867, 5,064,802,5,132,380, 5,321,106,5,470,993,5,486,632, WO 95/00526, WO 98/49212 and U. S. S. N. 60/005913.

In EP-A-514,828 certain borane derivatives of the foregoing catalysts were disclosed and a method for their preparation taught and claimed. In USP 5,453,410 combinations of cationic catalyst complexes with an alumoxane were disclosed as suitable olefin polymerization catalysts. Variously substituted indenyl containing metal complexes were taught in U. S. S. N. 592,756 filed January 26,1996 as well as in WO 95/14024.

The CGCs used in the practice of this invention comprise: A. 1) a metal complex of formula (1), and 2) an activating cocatalyst, the metal complex and the activating cocatalyst present in a molar ratio of 1: 10,000 to 100: 1, or B. the reaction product formed by converting a metal complex of formula (I) to an active catalyst by use of an activating technique.

Formula (I) is: ZLMXpX\ ( !) wherein M was a metal of Group 4 of the Periodic Table of the Elements having an oxidation state of +2, +3 or +4 bound in an q5 bonding mode to L; L was a cyclopentadienyl-, indenyl-, tetrahydroindenyl-, fluorenyl-, tetrahydrofluorenyl-, or octahydrofluorenyl-group covalently substituted with at least the divalent moiety, Z, and L further may be substituted with from 1 to 8 substituents independently selected from the group consisting of hydrocarbyl, halo, halohydrocarbyl, hydrocarbyloxy, dihydrocarbylamine, dihydrocarbylphosphino or silyl groups containing up to 20 nonhydrogen atoms; Z was a divalent moiety, or a moiety comprising one o-bond and a neutral two electron pair able to form a coordinate-covalent bond to M, Z comprising boron, or a

member of Group 14 of the Periodic Table of the Elements, and also comprising nitrogen, phosphorus, sulfur or oxygen; X was an anionic ligand group having up to 60 atoms exclusive of the class of ligands that were cyclic, delocalized, Tc-bound ligand groups; X'independently each occurrence was a neutral ligating compound having up to 20 atoms; p was 0,1 or 2, and was two less than the formal oxidation state of M, with the proviso that when X was a dianionic ligand group, p was 1; and q was 0, 1 or 2.

The metal complex of formula I was rendered catalytically active by combination with an activating cocatalyst or use of an activating technique.

In one embodiment, the metal complex was of formula 11 (ZLM*X*p*) *A- (II) wherein: M* was a metal of Group 4 of the Periodic Table of the Elements having an oxidation state of +3 or +4, bound in an il bonding mode to L; L was a cyclopentadienyl-, indenyl-, tetrahydroindenyl-, fluorenyl-, tetrahydrofluorenyl-, or octahydrofluorenyl-group covalently substituted with at least the divalent moiety, Z. and L further may be substituted with from 1 to 4 substituents independently selected from the group consisting of hydrocarbyl, halo, halohydrocarbyl, hydrocarbyloxy, dihydrocarbylamino, dihydrocarbylphosphino or silyl groups containing up to 20 nonhydrogen atoms; Z was a divalent moiety bound to both L and M* via 6-bonds, Z comprising boron, or a member of Group 14 of the Periodic Table of the Elements, and also optionally comprising nitrogen, phosphorus, sulfur or oxygen; X* was an anionic ligand group having up to 60 atoms exclusive of the class of ligands that were cyclic, delocalized, n-bond ligand groups; p* was 0 or 1, and was three less than the formal oxidation state of M; and A-was an inert, noncoordinating anion.

All reference to the Periodic Table of the Elements shall refer to the Periodic Table of the Elements published and copyrighted by CRC Press, Inc., 1995. Also, any

reference to a Group or Groups shall be to the Group or Groups as reflected in this Periodic Table of the Elements using the IUPAC system for numbering groups.

Zwitterionic complexes result from activation of a Group 4 metal diene complex, that is, complexes in the form of a metallocyclopentene wherein the metal was in the +4 formal oxidation state, by the use of a Lewis acid activating cocatalyst, especially tris (perfluoroaryl) borane compounds. These zwitterionic complexes were believed to correspond to formula (III): M was a Group 4 metal in the +4 formal oxidation state; L and Z were as previously defined; X** was the divalent remnant of the conjugated diene formed by ring opening at one of the carbon to metal bonds of a metallocyclopentene; and A was the moiety derived from the activating cocatalyst.

As used herein,"noncoordinating, compatible anion"means an anion which either does not coordinate to component A) or which was only weakly coordinated with A) and remains sufficiently labile to be displaced by a neutral Lewis base. A noncoordinating, compatible anion specifically refers to a compatible anion which when functioning as a charge balancing anion in one of the CGCs of dual CGC system, does not transfer an anionic substituent or fragment of the substituent to the cation to form a neutral four coordinate complex and a neutral metal byproduct."Compatible anions"were anions which were not degraded to neutrality when the initially formed complex decomposes and were noninterfering with desired subsequent polymerizations.

Preferred X'groups were phosphines, especially trimethylphosphine, triethylphosphine, triphenylphosphine and bis (1,2-dimethylphosphino) ethane; P (OR'") 3, wherein R iv was a hydrocarbyl group preferably containing 1 to 20 carbon atoms; ethers, especially tetrahydrofuran; amines, especially pyridine, bipyridine, tetramethylethylenediamine (TMEDA), and triethylamine; olefins, and conjugated dienes having from 4 to 40 carbon atoms. Complexes including the latter X'groups include those in which the metal was in the +2 formal oxidation state.

In one preferred embodiment, A) metal complexes used according to the present invention were complexes corresponding to formula (IV):

in which: R independently each occurrence was a group selected from hydrogen, hydrocarbyl, halohydrocarbyl, silyl, genmyl and mixtures thereof, said group containing up to 20 nonhydrogen atoms; M was titanium, zirconium or hafnium; Z was a divalent moiety comprising boron, or a member of Group 14 of the Periodic Table of the Elements, and also comprising nitrogen, phosphorus, sulfur or oxygen, said moiety having up to 60 nonhydrogen atoms; X and X'were as previously defined; p was 0,1 or 2; and q was 0 or 1; with the proviso that; when p was 2, q was 0, M was in the +4 formal oxidation state, and X was an anionic ligand selected from the group consisting of halide, hydrocarbyl, hydrocarbyloxy, di (hydrocarbyl) amido, di (hydrocarbyl) phosphido, hydrocarbylsulfido, and silyl groups, as well as halo-, di (hydrocarbyl) amino-, hydrocarbyloxy-and di (hydrocarbyl) phoshino- substituted derivatives thereof, said X group having up to 20 nonhydrogen atoms, when p was 1, q was 0, M was in the +3 formal oxidation state, and X was a stabilizing anionic ligand group selected from the group consisting of allyl, 2- (N, N- dimethylaminomethyl) phenyl, and 2- (N, N-dimethyl) aminobenzyl, or M was in the +4 formal oxidation state, and X was a divalent derivative of a conjugated diene, M and X together forming a metallocyclopentene group, and when p was 0, q was 1, M was in the +2 formal oxidation state, and X'was a neutral, conjugated or nonconjugated diene, optionally substituted with one or more hydrocarbyl groups, said X'having up to 40 carbon atoms and forming a z-complex with M.

More preferred A) coordination complexes of this embodiment were complexes corresponding to formula (V):

wherein R independently each occurrence was hydrogen or C,-6 alkyl; M was titanium; Y was-0-,-S-,-NR*-,-PR*- ; Z* was SiR*2, CR*2, SiR*2SiR*2, CR*2CR*2, CR*=CR*, CR*2SiR*2, or GeR*2; R* each occurrence was independently hydrogen, or a member selected from hydrocarbyl, hydrocarbyloxy, silyl, halogenated alkyl, halogenated aryl, and combinations thereof, and R* having up to 20 nonhydrogen atoms, and optionally, two R* groups from Z (when R* was not hydrogen), or an R* group from Z and an R* group from Y form a ring system; p was 0,1 or 2; q was 0 or 1; with the proviso that: when p was 2, q was 0, M was in the +4 format oxidation state, and X was independently each occurrence methyl or benzyl, when p was 1, q was 0, M was in the +3 formal oxidation state, and X was 2 (N, N- dimethyl) aminobenzyl; or M was in the +4 formal oxidation state and X was 1,4- butadienyl, and when p was 0, q was 1, M was in the +2 formal oxidation state, and X'was 1,4- diphenyl-1,3-butadiene or 1,3-pentadiene. The latter diene was illustrative of unsymmetrical diene groups that result in production of metal complexes that were actually mixtures of the respective geometrical isomers.

In another preferred embodiment, the A) metal complexes used according to the present invention were complexes corresponding to formula (VI):

where M was titanium, zirconium or hafnium in the +2, +3 or +4 formal oxidation state; R'and R"were independently each occurrence hydride, hydrocarbyl, silyl, genmyl, halide, hydrocarbyloxy, hydrocarbylsiloxy, hydrocarbylsilylamino, di (hydrocarbyl) amino, hydrocarbyleneamino, di (hydrocarbyl) phosphino, hydrocarbylene-phosphino, hydrocarbylsulfido, halo-substituted hydrocarbyl, hydrocarbyloxy-substituted hydrocarbyl, silyl-substituted hydrocarbyl, hydrocarbylsiloxy-substituted hydrocarbyl, hydrocarbylsilylamino-substituted hydrocarbyl, di (hydrocarbyl) amino-substituted hydrocarbyl, hydrocarbyleneamino-substituted hydrocarbyl, di (hydrocarbyl) phosphino- substituted hydrocarbyl, hydrocarbylene-phosphino-substituted hydrocarbyl, or hydrocarbylsulfido-substituted hydrocarbyl, said R'or R"group having up to 40 nonhydrogen atoms, and optionally two or more of the foregoing groups may together form a divalent derivative; R"'was a divalent hydrocarbylene-or substituted hydrocarbylene group forming a fused system with the remainder of the metal complex, said R"'containing from I to 30 nonhydrogen atoms; Z was a divalent moiety, or a moiety comprising one 6-bond and a neutral two electron pair able to form a coordinate-covalent bond to M, said Z comprising boron, or a member of Group 14 of the Periodic Table of the Elements, and also comprising nitrogen, phosphorus, sulfur or oxygen; X was a monovalent anionic ligand group having up to 60 atoms exclusive of the class of ligands that were cyclic, delocalized, n-bound ligand groups; X'independently each occurrence was a neutral ligating compound having up to 20 atoms; X"was a divalent anionic ligand group having up to 60 atoms; p was 0,1,2, or 3; q was 0,1 or 2, and

r was 0 or 1.

The number of X groups depends on the oxidation state of M, whether Z was divalent or not and whether any neutral diene groups or divalent X"groups were present. The skilled artisan will appreciate that the quantity of the various substituents and the identity of Z were chosen to provide charge balance, thereby resulting in a neutral metal complex. For example, when Z was divalent, and r was 0, p was two less than the formal oxidation state of M. When Z contains one neutral two electron coordinate-covalent bonding site, and M was in a formal oxidation state of +3, p may equal 0 and r equal 1, or p may equal 2 and r equal 0. In a final example, if M was in a formal oxidation state of +2, Z may be a divalent ligand group, p and r may both equal 0 and one neutral ligand group may be present.

The above complexes may exist as isolated crystals optionally in pure form or as a mixture with other complexes, in the form of a solvated adduct, optionally in a solvent, especially an organic liquid, as well as in the form of a dimer or chelated derivative thereof, wherein the chelating agent was an organic material such as ethylenediaminetetraacetic acid (EDTA).

Preferred coordination complexes for use as part of the second component of the dual CGC catalyst system were complexes corresponding to formula (VII) or (VIII): wherein: R'was hydrocarbyl, di (hydrocarbylamino), or a hydrocarbyleneamino group, said R'having up to 20 carbon atoms, R"was C-2o hydrocarbyl or hydrogen; M was titanium; Y was-0-,-S-,-NR*-,-PR*- ;-NR2*, or-PR2*; Z* was SiR*2, CR*2, SiR*2SiR*2, CR*2CR*2, CR*=CR*, CR*2SiR*2, or GeR*2;

R* each occurrence was independently hydrogen, or a member selected from hydrocarbyl, hydrocarbyloxy, silyl, halogenated alkyl, halogenated aryl, and combinations thereof, said R* having up to 20 non-hydrogen atoms, and optionally, two R* groups from Z (when R* was not hydrogen), or an R* group from Z and an R* group from Y form a ring system; X, X'and X"were as previously defined; p was 0,1 or 2; q was 0 or 1; and r was 0 or 1; with the proviso that: when p was 2, q and r were 0, M was in the +4 formal oxidation state (or M was in the +3 formal oxidation state if Y was-NR*2 or-PR*2), and X was an anionic ligand selected from the group consisting of halide, hydrocarbyl, hydrocarbyloxy, di (hydrocarbyl) amido, di (hydrocarbyl) phosphido, hydrocarbylsulfido, and silyl groups, as well as halo-, di (hydrocarbyl) amino-, hydrocarbyloxy-, and di (hydrocarbyl) phosphino-substituted derivatives thereof, said X group having up to 30 nonhydrogen atoms, when r was 1, p and q were 0, M was in the +4 formal oxidation state, and X"was a dianionic ligand selected from the group consisting of hydrocarbadiyl, oxyhydrocarbyl, and hydrocarbylenedioxy groups, said X group having up to 30 nonhydrogen atoms, when p was 1, q and r were 0, M was in the +3 formal oxidation state, and X was a stabilizing anionic ligand group selected from the group consisting of allyl, 2- (N, N- dimethylamino) phenyl, 2- (N, N-dimethylaminomethyl) phenyl, and 2- (N, N- dimethylamino) benzyl, and when p and r were 0, q was 1, M was in the +2 formal oxidation state, and X'was a neutral, conjugated or nonconjugated diene, optionally substituted with one or more hydrocarbyl groups, said X'having up to 40 carbon atoms and forming an-complex with M. Most preferred metal complexes were those according to the previous formula (XIV) or (XV), wherein M, X, X', X", R'R", Z*, Y, p, q and r were as previously defined, with the proviso that: when p was 2, q and r were 0, M was in the +4 formal oxidation state, and X was independently each occurrence methyl, benzyl, or halide; when p and q were 0, r was one, and M was in the +4 formal oxidation state, X" was a 1,4-butadienyl group that forms a metallocyclopentene ring with M,

when p was 1, q and r were 0, M was in the +3 formal oxidation state, and X was 2- (N, N-dimethylamino) benzyl; and when p and r were 0, q was 1, M was in the +2 formal oxidation state, and X'was 1,4-diphenyl-1,3-butadiene or 1,3-pentadiene.

Especially preferred coordination complexes corresponding to the previous formulas (XIV) and (XV) were uniquely substituted depending on the particular end use thereof. In particular, highly useful metal complexes for use in catalyst compositions for the copolymerization of ethylene, one or more monovinyl aromatic monomers, and optionally an a-olefin or diolefin comprise the foregoing complexes (XIV) or (XV) wherein R'was C6 20 aryl, especially phenyl, biphenyl or naphthyl, and R"was hydrogen or methyl, especially hydrogen. More preferably such complexes were 3-phenyl- substituted s-indecenyl complexes corresponding to formulae (IX) or (X): Highly useful metal complexes for use in the second component of the dual CGC catalyst system comprise the foregoing complexes (XIV) or (XV) wherein R'was Cl 4 alkyl, N, N-dimethylamino or 1-pyrrolidinyl, and R"was hydrogen or Cl 4 alkyl.

Moreover, in such complexes, Y was preferably a cyclohexylamido group, X was methyl, p was two, and both q and r is 0. Most preferably such complexes were 2,3-dimethyl- substituted s-indecenyl complexes corresponding to formula (XI) or (XII):

Finally, highly useful metal complexes for use in the second component of the dual CGC catalyst system for the copolymerization of ethylene, an a-olefin and a diene, especially ethylene, propylene and a nonconjugated diene, such as ethylidenenorbomene or 1,4-hexadiene, comprise the foregoing complexes (XIV) or (XV) wherein R'was hydrogen, and R"was C, 4 alkyl, especially methyl. Most preferred were 2-methyl- substituted s-indecenyl complexes corresponding to formula (XIII) or (XIV): Illustrative metal complexes that may be employed in the preparation of the second component of the dual CGC systems of the present invention were further described in WO 98/27103.

The metal complexes used in the practice of this invention were prepared by well- known synthetic techniques. One preferred process for preparing the metal complexes was disclosed in USP 5,491,246. The reactions were conducted in a suitable noninterfering solvent at a temperature from-100 to 300 C, preferably from-78 to 100 C, most preferably from 0 to 50 C. A reducing agent may be used to cause M to be reduced from a higher to a lower oxidation state. Examples of suitable reducing agents were alkali metals, alkaline earth metals, aluminum and zinc, alloys of alkali metals or alkaline earth metals such as sodium/mercury amalgam and sodium/potassium alloy, sodium

naphthalenide, potassium graphite, lithium alkyls, lithium or potassium alkadienyls, and Grignard reagents.

Suitable reaction media for the formation of the complexes include aliphatic and aromatic hydrocarbons, ethers, and cyclic ethers, particularly branched chain hydrocarbons such as isobutane, butane, pentane, hexane, heptane, octane, and mixtures thereof ; cyclic and alicyclic hydrocarbons such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof ; aromatic and hydrocarbyl substituted aromatic compounds such as benzene, toluene, and xylene, Cl 4 dialkyl ethers, Cl 4 dialkyl ether derivatives of (poly) alkylene glycols, and tetrahydrofuran. Mixtures of the foregoing were also suitable.

Suitable activating cocatalysts useful in combination with the A) metal complexes were those compounds capable of abstraction of an X substituent from A) to form an inert, noninterfering counter ion, or that form a zwitterionic derivative of A). Suitable activating cocatalysts for use herein include perfluorinated tri (aryl) boron compounds, and most especially tris (pentafluorophenyl) borane; nonpolymeric, compatible, noncoordinating, ion-forming compounds (including the use of such compounds under oxidizing conditions), especially the use of ammonium, phosphonium, oxonium, carbonium, silylium or sulfonium salts of compatible, noncoordinating anions, and ferritenium salts of compatible, noncoordinating anions. Suitable activating techniques include the use of bulk electrolysis (explained subsequently in more detail). A combination of the foregoing activating cocatalysts and techniques may be employed as well. The foregoing activating cocatalysts and activating techniques have been previously taught with respect to different metal complexes in the following references: EP-A- 277,003, USP 5,153,157, USP 5,064,802, EP-A-468,651, USP 5,721,185, USP 5,350,723. More particularly, suitable ion-forming compounds useful as cocatalysts in one embodiment of the present invention comprise a cation which was a Bronsted acid capable of donating a proton, and a compatible, noncoordinating anion, A-.

Preferred anions were those containing a single coordination complex comprising a charge-bearing metal or metalloid core which anion was capable of balancing the charge of the active catalyst species (the metal cation) which may be formed when the two components were combined. Also, the anion should be sufficiently labile to be displaced by olefinic, diolefinic and acetylenically unsaturated compounds or other neutral Lewis bases such as ethers or nitrites. Suitable metals include, but were not limited to,

aluminum, gold and platinum. Suitable metalloids include, but were not limited to, boron, phosphorus, and silicon. Compounds containing anions which comprise coordination complexes containing a single metal or metalloid atom were, of course, well known and many, particularly such compounds containing a single boron atom in the anion portion, were available commercially. Preferably such cocatalysts may be represented by general formula (XV): (L*-H) d* (A) d- (XV) wherein: L* was a neutral Lewis base; (L*-H) + was a Bronsted acid; Ad-is a noncoordinating, compatible anion having a charge of d-, and d was an integer from 1-3.

More preferably Ad-corresponds to formula (XVI): [M'Q4]- (XVI) wherein: M'was boron or aluminum in the formal +3 formal oxidation state; and Q independently each occurrence was selected from hydrie, dialkylamido, halide, hydrocarbyl, hydrocarbyloxide, halosubstituted hydrocarbyl, halosubstituted hydrocarbyloxy, and halosubstituted silylhydrocarbyl radicals (including perhalogenated hydrocarbyl perhalogenated hydrocarbyloxy-and perhalogenated silylhydrocarbyl radicals), said Q having up to 20 carbons with the proviso that in not more than one occurrence was Q halide. Examples of suitable hydrocarbyloxide Q groups were disclosed in USP 5,296,433.

In a more preferred embodiment, d was 1, that is, the counter ion has a single negative charge and was A-. Activating cocatalysts comprising boron which were particularly useful in the preparation of the first catalyst component of this invention may be represented by general formula (XVII): (L*-H) + (BQ4)- (XVII)

wherein: L* was as previously defined; B was boron in a formal oxidation state of 3; and Q was a hydrocarbyl-, hydrocarbyloxy-, fluorinated hydrocarbyl-, fluorinated hydrocarbyloxy-, or fluorinated silylhydrocarbyl-group of up to 20 nonhydrogen atoms, with the proviso that in not more than one occasion was Q hydrocarbyl.

Most preferably, Q was each occurrence a fluorinated aryl group, especially, a pentafluorophenyl group.

Illustrative, but not limiting, examples of boron compounds which may be used as an activating cocatalyst in the preparation of the improved catalysts of this invention were trisubstituted ammonium salts such as: trimethylammonium tetrakis (pentafluorophenyl) borate, triethylammonium tetrakis (pentafluorophenyl) borate, tripropylammonium tetrakis (pentafluorophenyl) borate, tri (n-butyl) ammonium tetrakis (pentafluorophenyl) borate, tri (sec-butyl) ammonium tetrakis (pentafluorophenyl) borate, N, N-dimethylanilinium tetrakis (pentafluorophenyl) borate, N, N-dimethylanilinium n-butyltris (pentafluorophenyl) borate, N, N-dimethylanilinium benzyltris (pentafluorophenyl) borate, N, N-dimethylanilinium tetrakis (4- (t-butyldimethylsilyl)-2,3,5,6-tetrafluorophenyl) borate, N, N-dimethylanilinium tetrakis (4- (triisopropysilyl)-2,3,5,6-tetrafluorophenyl) borate, N, N-di (n-hexadecanyl)-N- methylammonium tetrakis (2,3,4,5,6-pentafluorophenyl) borate, N, N-dimethylanilinium pentafluorophenoxytris (pentafluorphenyl) borate, N, N-diethylanilinium tetrakis (pentafluorphenyl) borate, N, N-dimethyl-2,4,6-trimethylanilinium tetrakis (pentafluorophenyl) borate, trimethylammonium tetrakis (2,3,4,6-tetrafluorophenyl) borate, triethylammonium tetrakis (2,3,4,6-tetrafluorophenyl) borate, tripropylammonium tetrakis (2,3,4,6-tetrafluorophcnyl) borate, tri (n-butyl) ammonium tetrakis (2,3,4,6- tetrafluorophenyl) borate, dimethyl (t-butyl) ammonium tetrakis (2,3,4,6-tetrafluorophenyl) borate, N, N-dimethylanilinium tetrakis (2,3,4,6-tetrafluorophenyl) borate, N, N- diethylanilinium tetrakis (2,3,4,6-tetrafluorophenyl) borate, and N, N-dimenhyl-2,4,6- trimethylanilinium tetrakis (2,3,4,6-tetrafluorophenyl) borate; disubstituted ammonium salts such as: di- (i-propyl) ammonium tetrakis (pentafluorophenyl) borate, and dicyclohexylammonium tetrakis (pentafluorophenyl) borate; trisubstituted phosphonium salts such as: triphenylphosphonium tetrakis (pentafluorophenyl) borate, tri (o-tolyl) phosphonium tetrakis (pentafluorophenyl) borate, and tri (2,6-dimethylphenyl) phosphonium tetrakis (pentafluorophenyl) borate; disubstituted oxonium salts such as: diphenyloxonium

tetrakis (pentafluorophenyl) borate, di (o-tolyl) oxonium tetrakis (pentafluororphenyl) borate, and di (2,6-dimethylphenyl oxonium tetrakis (pentafluorophenyl) borate; disubstituted sulfonium salts such as: diphenylsulfonium tetrakis (pentafluorophenyl) borate, di (o-tolyl) sulfonium tetrakis (pentafluorophenyl) borate, and bis (2,6-dimethylphenyl) sulfonium tetrakis (pentafluorophenyl) borate.

Preferred (L*-H) + cations were N, N-dimethylanilinium, tributylammonium and N, N-di (n-hexadecanyl)-N-methylammonium.

Another suitable ion forming, activating cocatalyst comprises a salt of a cationic oxidizing agent and a noncoordinating, compatible anion represented by formula (XVIII): (OX) d (A) e (XVIII) wherein: Ox was a cationic oxidizing agent having a charge of e+; e was an integer from 1 to 3; and Ad-and d were as previously defined.

Examples of cationic oxidizing agents include: ferrocenium, hydrocarbyl- substituted ferrocenium, Ag+ or Pb. Preferred embodiments of Ad-were those anions previously defined with respect to the Bronsted acid containing activating cocatalysts, especially tetrakis (pentafluorophenyl) borate.

Another suitable ion forming, activating cocatalyst comprises a compound which was a salt of a carbenium ion and a noncoordinating, compatible anion represented by the formula (XIX): (D) + A- wherein: (C) + was ion CI-20 carbenium A-was as previously defined. A preferred carbenium ion was the trityl cation, that is triphenylmethylium.

A further suitable ion forming, activating cocatalyst comprises a compound which was a salt of a silylium ion and a noncoordinating, compatible anion represented by formula (XX): RV3Si*A- (XX)

wherein: Rv was Cl l0 hydrocarbyl, and A'was as previously defined.

Preferred silylium salt activating cocatalysts were trimethylsilylium tetrakis (pentafluorophenyl) borate, triethylsilylium tetrakis (pentafluorophenyl) borate and ether substituted adducts thereof. Silylium salts have been previously generically disclosed in J. Chem Soc. Chem. Comm., 1993,383-384, as well as Lambert, J. B., et al, Organometallics, 1994,13,2430-2443. The use of the above silylium salts as activating cocatalysts for addition polymerization catalysts as claimed in USP 5,625,087.

Certain complexes of alcohols, mercaptans, silanols, and oximes with tris (pentafluorophenyl) borane were also effective catalyst activators and may be used according to the present invention. Such cocatalysts were disclosed in USP 5,296,433.

The technique of bulk electrolysis involves the electrochemical oxidation of the metal complex under electrolysis conditions in the presence of a supporting electrolyte comprising a noncoordinating, inert anion. In the technique, solvents, supporting electrolytes and electrolytic potentials for the electrolysis were used such that electrolysis byproducts that would render the metal complex catalytically inactive were not substantially formed during the reaction. More particularly, suitable solvents were materials that were (i) liquids under the conditions of the electrolysis (generally temperatures from 0 to 100 C), (ii) capable of dissolving the supporting electrolyte, and (iii) inert."Inert solvents"were those that were not reduced or oxidized under the reaction conditions employed for the electrolysis. It was generally possible in view of the desired electrolysis reaction to choose a solvent and a supporting electrolyte that were unaffected by the electrical potential used for the desired electrolysis. Preferred solvents include difluorobenzene (all isomers), dimethoxyethane (DME), and mixtures thereof.

The electrolysis may be conducted in a standard electrolytic cell containing an anode and cathode (also referred to as the working electrode and counterelectrode respectively). Suitable materials of construction for the cell were glass, plastic, ceramic and glass-coated metal. The electrodes were prepared from inert conductive materials, by which were meant conductive materials that were unaffected by the reaction mixture or reaction conditions. Platinum or palladium were preferred inert conductive materials.

Normally an ion permeable membrane such as a fine glass grit separates the cell into separate compartments, the working electrode compartment and counterelectrode

compartment. The working electrode was immersed in a reaction medium comprising the metal complex to be activated, solvent, supporting electrolyte, and any other materials desired for moderating the electrolysis or stabilizing the resulting complex. The counterelectrode was immersed in a mixture of the solvent and supporting electrolyte.

The desired voltage may be determined by theoretical calculations or experimentally by sweeping the cell using a reference electrode such as silver electrode immersed in the cell electrolyte. The background cell current, the current draw in the absence of the desired electrolysis, was also determined. The electrolysis was completed when the current drops from the desired level to the background level. In this manner, complete conversion of the initial metal complex can be easily detected.

Suitable supporting electrolytes were salts comprising a cation and a compatible, noncoordinating anion, A-. Preferred supporting electrolytes were salts corresponding to the formula G+A-wherein G+ was a cation which was nonreactive towards the starting and resulting complex, and A-was as previously defined.

Examples of cations, G+, include tetrahydrocarbyl substituted ammonium or <BR> <BR> <BR> <BR> phosphonium cations having up to 40 nonhydrogen atoms. Preferred cations were the tetra(n-butylammonium)- and tetraethylammonium-cations During activation of the complexes of the present invention by bulk electrolysis the cation of the supporting electrolyte passes to the counterelectrode and A-migrates to the working electrode to become the anion of the resulting oxidized product. Either the solvent or the cation of the supporting electrolyte was reduced at the counterelectrode in equal molar quantity with the amount of oxidized metal complex formed at the working electrode. Preferred supporting electrolytes were tetrahydrocarbylammonium salts of tetrakis (perfluoroaryl) borates having from I to 10 carbons in each hydrocarbyl or perfluoroaryl group, especially tetra (n-butylammonium) tetrakis (pentafiuorophenyl) borate.

A further recently discovered electrochemical technique for generation of activating cocatalysts was the electrolysis of a disilane compound in the presence of a source of a noncoordinating compatible anion. All of the foregoing techniques were more fully disclosed and claimed in USP 5,372,682. In as much as the activation technique ultimately produces a cationic metal complex, the amount of such resulting complex formed during the process can be readily determined by measuring the quantity of energy used to form the activated complex in the process.

Alumoxanes, especially methylalumoxane or triisobutylaluminum modified methylalumoxane were also suitable activators and may be used for activating the present metal complexes.

Preferred activating cocatalysts include trispentafluorophenylborane and di (hydrogenated-tallowalkyl) methyl ammonium tetrakis- (pentafluorophenyl) borate.

The molar ratio of metal complex: activating cocatalyst employed preferably ranges from 1: 1000 to 2: 1, more preferably from 1: 5 to 1.5: 1, most preferably from 1: 2 to 1: 1.

The amount of first CGC to second CGC in the mixed catalyst system can vary widely and to convenience. Typically, the minimum ratio, in weight percent based on the combined weight of the metals, of first CGC to second CGC was 1: 99, preferably 5: 95 and most preferably 75: 25. The typical maximum ratio, again in weight percent based on the combined weight of the metals, was 99: 1, preferably 95: 5 and most preferably 25: 75.

The reactivity ratios describe the copolymerization of the monomers M, and M2 as shown in the following equations where M, was ethylene and M2 was a higher a-olefin.

The value of r, was used to describe the reactivity of a catalyst to comonomers with a lower value of r, indicating greater reactivity for comonomer incorporation. kil M,. +M,M2 (1) <BR> <BR> <BR> <BR> <BR> kil<BR> <BR> <BR> +M2#M2(2)M1# <BR> <BR> <BR> <BR> <BR> <BR> <BR> <BR> kil<BR> <BR> <BR> +M2#M2(3)M2# kil M2 o + M, 9 M, (4) <BR> <BR> =7/2(5)<BR> <BR> <BR> =2//(6) The comonomer concentration in the polymer and reactor were then related by: <M/M/r/M/+M2!/ (7) dM2 M2 r2 M2 + M, m2

where M 1 and M2 refer to the reactor concentrations, and m 1 and m2 refer to the polymer composition.

The reactivity ratios can be obtained using the Fineman-Ross method in which the monomer concentrations in the reactor and in the final polymer were related at low conversions by solving equation (7) graphically and obtaining r as the slope and the intercept being minus r2.

The lower the value of r,, the closer were the monomer and comonomer in reactivity, and the greater the incorporation rate of the comonomer. When two catalysts that differ in the value of r, were used together in a single reaction vessel to promote the same ethylene/a-olefin polymerization, a polymer blend will be produced, that is, a product comprising two polymer components differing in molecular architecture. The polymer component produced through the action of the catalyst with the lower reactivity ratio will contain more comonomer than the polymer component produced through the action of the catalyst with the higher reactivity ratio. For purposes of describing this invention, catalysts with reactivity ratios that differ by more than 50 percent from one another with respect to the polymerization of ethylene and a given a-olefin at the same temperature will produce a polymer blend in which the blend components do not have a substantially uniform molecular architecture, and catalysts with reactivity ratios that differ by 50 percent or less, preferably 30 percent or less, from one another with respect to the polymerization of ethylene and a given a-olefin at the same temperature will produce a polymer blend in which the blend components do have a substantially uniform molecular architecture. For interpolymer blends derived from three or more comonomers, particularly those interpolymer blends in which one of the comonomers was a polyene, the molecular architecture of the blend components may not be substantially uniform even though the reactivity ratios of the catalysts differ by less than 50 percent with respect to ethylene and the a-olefin because the reactivity ratios of the catalysts may differ by more than 50 percent with respect to ethylene and the second comonomer.

In general, the polymerization may be accomplished at conditions well known in the prior art for Ziegler-Natta or Kaminsky-Sinn type polymerization reactions, that is, temperatures from 0-250 C, preferably 30 to 200 C and pressures from atmospheric to

10,000 atmospheres. Suspension, solution, slurry, gas phase, solid state powder polymerization or other process conditions may be employed if desired. A support, especially silica, alumina, or a polymer (especially poly (tetrafluoroethylene) or a polyolefin) may be employed, and desirably was employed when the catalysts were used in a gas phase polymerization process. The support was preferably employed in an amount to provide a weight ratio of catalyst (based on metal): support from 1: 100,000 to 1: 10, more preferably from 1: 50,000 to 1: 20, and most preferably from 1: 10,000 to 1: 30.

In most polymerization reactions the molar ratio of catalyst : polymerizable compounds employed was from 10-12: 1 to 10-l: 1, more preferably from 10-9: 1 to 10-5: 1.

In this ratio,"catalyst"means the mixed catalyst system. Suitable solvents for solution polymerization were inert liquids. Examples include straight and branched-chain hydrocarbons such as isobutane, butane, pentane, hexane, heptane, octane, and mixtures thereof ; cyclic and alicyclic hydrocarbons such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof ; perfluorinated hydrocarbons such as perfluorinated C4 10 alkanes, and alkyl-substituted aromatic compounds such as benzene, toluene, xylene, and ethylbenzene. Suitable solvents also include liquid olefins that may act as monomers or comonomers.

Utilizing the mixed catalyst system of the present invention, a-olefin homopolymers and copolymers having densities from 0.85 g/cm3 to 0.97 g/cm3, and Mooney viscosities of from less than 0.01 to 150 were readily attained in a highly efficient process.

The mixed catalyst systems of the present invention were particularly advantageous for the production of ethylene homopolymers and ethylene/a-olefin copolymers having long chain branching, often high levels of long chain branching. The use of this system in continuous polymerization processes, especially continuous, solution polymerization processes, allows for elevated reactor temperatures which favor the formation of vinyl terminated polymer chains that may be incorporated into a growing polymer, thereby giving a long chain branch. Although relatively large amounts of a- olefin disfavor the formation of long chain branches, the polymerization conditions can be adjusted as taught in PCT/US97/07252 to offset, at least partially, this tendency. The use of the present catalyst compositions advantageously allows for the economical production

of ethylene/a-olefin copolymers having processability similar to high pressure, free radical produced low-density polyethylene.

The mixed catalyst systems used in this invention may also be advantageously employed to prepare olefin polymers having improved processing properties by polymerizing ethylene alone or ethylene/a-olefin mixtures with low levels of a"H" branch inducing diene, such as norbornadiene, 1,7-octadiene, or 1,9-decadiene. The unique combination of elevated reactor temperatures, high molecular weight (or low melt indices) at high reactor temperatures and high comonomer reactivity advantageously allows for the economical production of polymers having excellent physical properties and processability. Preferably such polymers comprise ethylene, a C3 20 a-olefin and a "H"-branching comonomer. Preferably, such polymers were produced in a solution process, most preferably a continuous solution process.

The individual catalyst components of the mixed catalyst system may be prepared as a homogeneous catalyst by addition of the requisite components to a solvent in which polymerization will be carried out by solution polymerization procedures. These catalyst components may also be prepared and employed as a heterogeneous catalysts by adsorbing the requisite components on an inert inorganic or organic particulated solid.

Examples of such solids include, silica, silica gel, alumina, trialkylaluminum compounds, and organic or inorganic polymeric materials, especially polyolefins. In an preferred embodiment, a heterogeneous catalyst was prepared by coprecipitating the metal complex, an inert, inorganic compound and an activator, especially an ammonium salt of a hydroxyaryl (trispentafluorophenyl) borate, such as an ammonium salt of (4-hydroxy-3,5- ditertiarybutylphenyl) (trispentafluorophenylborate. A preferred inert, inorganic compound for use in this embodiment was a tri (C 4 alkyl) aluminum compound.

When prepared in heterogeneous or supported form, the catalyst compositions were employed in a slurry or gas phase polymerization. As a practical limitation, slurry polymerization takes place in liquid diluents in which the polymer product was substantially insoluble. Preferably, the diluent for slurry polymerization was one or more hydrocarbons with less than 5 carbon atoms. If desired, saturated hydrocarbons such as ethane, propane or butane may be used in whole or part as the diluent. Likewise the a- olefin monomer or a mixture of different a-olefin monomers may be used in whole or part

as the diluent. Most preferably at least a major part of the diluent comprises the a-olefin monomer or monomers to be polymerized.

At all times, the individual ingredients as well as the recovered catalyst components must be protected from oxygen and moisture. Therefore, the catalyst components and catalysts must be prepared and recovered in an oxygen and moisture free atmosphere. Preferably, therefore, the reactions were performed in the presence of an dry, inert gas such as, for example, nitrogen.

The polymerization may be carried out as a batchwise or a continuous polymerization process. A continuous process was preferred, in which event the mixed catalyst system, ethylene, comonomer, and optionally solvent were continuously supplied to the reaction zone and from which polymer product was continuously removed.

Without limiting in any way the scope of the invention, one means for carrying out such a polymerization process was as follows: In a stirred-tank reactor, the monomers to be polymerized were introduced continuously together with solvent and an optional chain transfer agent. The reactor contains a liquid phase composed substantially of monomers together with any solvent or additional diluent and dissolved polymer. If desired, a small amount of a"H"-branch inducing diene such as norbomadiene, 1,7-octadiene or 1,9- decadiene may also be added. The metal complexes and cocatalysts of the mixed catalyst system were continuously introduced into the reactor liquid phase.

The reactor temperature and pressure were controlled by adjusting the solvent/monomer ratio, the catalyst addition rate, as well as by cooling or heating coils, jackets or both. The polymerization rate was controlled by the rate of catalyst addition.

The ethylene content of the polymer product was detennined by the ratio of ethylene to comonomer in the reactor, which was controlled by manipulating the respective feed rates of these components to the reactor. The polymer product molecular weight was controlled, optionally, by controlling other polymerization variables such as the temperature, monomer concentration, or by the previously mention chain transfer agent, such as a stream of hydrogen introduced to the reactor, as was well known in the art.

The reactor effluent was contacted with a catalyst kill agent such as water or alcohol. The polymer solution was optionally heated, and the polymer product was recovered by flashing off gaseous monomers as well as residual solvent or diluent at reduced pressure, and, if necessary, conducting further devolatilization in equipment such as a devolatilizing extruder. In a continuous process the mean residence time of the

catalyst and polymer in the reactor generally was from 5 minutes to 8 hours, and preferably from 10 minutes to 6 hours. By using a mixed catalyst system that incorporates large amounts of hindered monovinyl monomer, hindered monovinyl homopolymer formed from residual quantities of the monomer were substantially reduced.

In one embodiment of this invention, the single reaction vessel in which the polymer blend was prepared was one reactor of a multiplicity of reactors deployed either in parallel or in series. In such deployments, the polymer blend of the single reaction vessel can be a feed to a subsequent reactor (series deployment), or it can be blended with the output from another reactor (parallel deployment).

The polymer blends of this invention have a wide range of uses. The blends were useful in the manufacture of molded articles such as toys, toy parts, sporting goods, medical goods, soft touch parts of a relatively low shore A hardness, and automotive parts, and extruded goods such as tubing and profiles. Other applications for these blends include wire and cable, footwear, building and construction materials, adhesives, films and fibers, flooring, foams, weather stripping, oil modification, general rubber goods, extruded sheets, instrument panel skins, food packaging, electronic components and the like. These blends can be crosslinked by any of the various crosslinking agents, for example, peroxide, sulfur, phenolics, azides and radiation, and/or grafted using maleic anhydride, silane or one or more of the other reactive monomers which can modify the functional performance of the blend. These blends can also be mixed with other materials such as thermoplastic olefins, elastomers and vulcanizates for use in various extrusion, injection molding, calendering, rotomolding, slush molding, blow molding, thermoforming and compression molding applications.

Examples The skilled artisan will appreciate that the present invention disclosed may be practiced in the absence of any component which has not been specifically disclosed. The following examples were provided as further illustration of the invention and were not to be construed as limiting. Unless stated to the contrary all parts and percentages were expressed on a weight basis.

Batch Reactor Run Description Additive solution: The additive solution was prepared by dissolving PEPQ (an antioxidant from Sandoz) and Irganox 1076 (a hindered phenolic antioxidant from Ciba- Geigy) in 500 ml of toluene. The concentration of the solution was 20 mg of total additive per I ml of solution.

Polymerization: A typical run using a mixed catalyst system was described. A one-gallon stirred reactor was charged with Isopar E (mixed alkanes; available from Exxon Chemicals Inc.), octene-1, hydrogen and, if desired, 5-ethylidene-2-norbornene (ENB). If ENB was added, then it was added to the reactor prior to the addition of hydrogen. All liquid components were measured by mass flow. The reactor was heated to the desired temperature and saturated with ethylene.

The catalyst was prepared in a drybox by syringing together the appropriate components with additional solvent to give a total volume of 18 ml. In mixed catalyst runs, the two components were added in molar ratio of metal (1 to 1 unless stated otherwise in the Tables). The catalyst solution was then transferred by syringe to a catalyst addition loop and injected into the reactor over approximately 4 minutes using a flow of high-pressure solvent. An exotherm of 10 C was observed. The polymerization was allowed to proceed for 10 minutes while feeding ethylene on demand to maintain a relatively constant pressure (typically between 450 and 465 psi. The maximum flow of ethylene was typically 20 g/min. The amount of ethylene consumed during the reaction was monitored using a mass flowmeter.

The polymer solution was then dumped from the reactor into a nitrogen-purged glass kettle. An aliquot of the additive solution described above was added to this kettle and the solution stirred thoroughly (the amount of additive used was chosen based on the total ethylene consumed during the polymerization to produce 1000 ppm of each additive in the polymer). The polymer solution was dumped into a tray, air dried overnight, then thoroughly dried in a vacuum oven for one day. Some of the polymers and polymer blends were then measured according to ASTM tests for tensile @ break, elongation @ break, 12 and I 10.

Table 1A reports the batch reactor preparation of ethylene/I-octene polymer blends and polymers using two mixed catalyst systems (A/B in Runs 1-6, and B/C in Runs 7-9) and the individual catalyst components of the systems, respectively, along with selected physical characteristics of the polymers and polymer blends. Runs 4-6 were

conducted at a temperature of 20 C greater than Runs 1-3. Runs 3 and 6 were representative of the process and polymer blends of this invention. Run 9 reports a comparative process and polymer blend. Tables 1 B, 1 C and ID report similar information for ethylene/propylene/ENB, ethylene/butene/ENB and ethylene butene polymer blends and polymers.

TABLE 1A Batch Reactor Operational Data and Polymer Blend Properties of Ethylene/1-Octene Polymers and Polvmer Blends

RunNumber 1 2 3 4 5 6 A/BBAA/BBCatalyst*A Temp, C 89. 5 89. 4 89. 9 109. 9 109. 8 109.9 1-Octene, g 351. 4 351. 1 350.9 450. 2 451. 2 450.1 Ti, µmole 1.50 1.25 1.25 1. 75 1.75 1.50 B/Ti 4. 00 3. 96 3. 96 4. 03 4. 03 4.00 Al/Ti 5. 00 5. 20 5. 20 5. 14 5. 14 5.00 Exotherm C 8. 7 9. 2 6. 0 4. 1 8. 2 5.3 C Flow, max 20. 1 19. 7 15. 8 21. 3 25. 0 20.6 C2 rate end 0 0. 4 0 0 0 0 C, used, 54.8 59.4 52.1 43.3 62.8 50. 5 Calculated Efficiency 763, 105 992, 506 870, 864 516v887 749, 018 7037031 Solvent, 1505.41500.21402.71402.31405.01504.3 Pressure, psig 457. 4 456. 8 458. 1 456.3 456. 6 456. 1 C2 load, 212.0 214.6 212.6 181.0 182. 5 182.2 444.3443.8445.6437.7439.7439.2C2pressure,psig H2 mmole 8. 0 8. 0 8. 0 8. 1 8. 2 8.2 Mw 72, 400 130. 700 198, 800 49, 500 87, 000 125,200 Mn 39, 100 54, 600 102, 500 25, 800 35, 800 63,000 MWD 1. 85 2. 39 1. 94 1. 92 2. 43 1.99 Mwl-222, 827--150, 081- 74,454--51,747-Mw2- MW Ratio Hi/Lo-2. 99--2. 90- Iz 6. 27 0. 796 0. 16 30. 99 4. 35 0.99 o 38. 62 6. 00 0. 93 188. 02 33. 35 6.41 7.55.86.17.76.5I10/I26.2 DSC Tm Peak Melting 67. 69 62. 97 59. 91 65. 42 59. 65 50.95 % Crystallized 23. 09 19. 85 17. 89 21. 07 19. 58 15.06 DSC Tg-51.69-54.99-51.35-52.56-53.47-58.13 Tc (onset) 53.03 50. 35 48. 58 53. 19 48. 31 40.37 Tc (peak) 50.09 47. 89 45. 95 47. 24 44. 13 36.18 J/g 70. 05 61. 26 53. 02 54. 55 54. 49 48.64 *A- (t-butylamido) dimethyl(tetramethylcyclopentadienyl)silanetitanium 1, 3-pentadiene.

B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

TABLE 1A (Cont'd) Batch Reactor Operational Data and Polymer Blend Properties of Ethylene/1-Octene Polymers and Polymer Blends Run Number-7 8 9 (Com) Catalyst*BCC/B Temp, C 109. 9 110. 1 109.6 Octene, g 750.7 750.9 750.6 Ti, pmole 1.50 1.50 1.40 B/Ti 4.00 4.00 3.96 Al/Ti 5.00 5.00 5.00 Exotherm C 3.5 3.9 1.9 C2 Flow, max 17.1 22. 3 10.2 C rate end 0 0. 1 0.2 C2 used, g 38.7 28. 3 13. 1 Calculated Efficiency 538,701 393,199 196,149 Solvent, g 1078.2 1081. 2 1081.5 Pressure, psig 456.1 455.5 456.3 C2 load, g 185. 7 184.9 186.6 443.4442.1443.4C2press H2 mmole 1. 6 1. 6 1. 6 Mw 142,400 324,700 253,600 Mn 74,100 182, 000 104,000 MWD 1. 92 1.78 2.44 Mwl--359, 791 -124,571Mw2- MW Ratio Hi/Lo--2.89 DSC Peak Melting Broad 66.51 78.38 % Crystallized 10. 23 23.20 20.19 DSC Tg-59.77-46.05-61.49 Tc (onset) #1 10.10 66. 51 68.39 Peak Cooling #1 0. 31 63.94 65.79 J/G #1 30.54 67.74 54.56 Tc (onset) --- Peak Cooling #2-0.89 * B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

C [N-(1,1-dimethylethyl)-1,1-dimethyl-1-((1,2,3,3a,7a-h)-3-(1- pyrrolidinyl)-1H-inden- 1-yl) silanaminato- (2-)-N] [ (2,3,4,5,-h)-2,4-pentadiene)]-titanium.

As the data of Runs 1-6 shows, polymer blends made with a mixed catalyst system have a larger MWD than the polymers made under similar polymerization conditions with only one of the mixed catalyst components (compare Runs I and 2 with 3; and Runs 4 and 5 with 6). Moreover, the polymer blends of Runs 3 and 6 have a substantially uniform molecular architecture as demonstrated by a single DSC Tm melting peak. In contrast, although Runs 7-9 also report that the blend has a larger MWD than the polymers made under similar polymerization conditions with only one of the mixed catalyst components (compare Runs 7 and 8 with 9), the components of the blend do not have a substantially uniform molecular architecture as demonstrated by the presence of two DSC peaks (note Peak Cooling #2). These results were consistent with the similarity in reactivity ratios of Catalysts A and B, and the dissimilarity in reactivity ratios between Catalysts B and C, with respect to ethylene and 1-octene, all as reported in Table 7A.

Also of interest was the fact that the high Mw/low Mw ratio was relatively constant over Runs 3,6 and 9 despite a 20 C temperature difference and the use of catalysts, that is, A and B vs. C, of different reactivity ratios (as reported in Table 7A). In addition, the I, o/I2 (rheology ratio) of the polymer blends made by the mixed catalyst system shows higher shear sensitivity which equates to improved processability in injection molded, extrusion or blow molded applications.

TABLE 1B Batch Reactor Operational Data and Physical Properties of Ethylene/Propylene/ENB Polymers and Polymer Blends Run Percent Percent Propylene ENB Temp, C H2 mmol Ethylene Ethylene Number Catalyst Catalyst mass, g mass, g mass, g partial A* B* pressure, si 10 100% 0% 200. 8 40. 2 99.8 12.50 143.7 318.3 11 75% 25% 200 40.3 99.9 12.10 148.6 321.4 12 50% 50% 202 40.1 100.3 12.00 149.5 328.8 13 25% 75% 201.2 40.3 99. 7 12.2 149.6 329.7 14 0% 100% 201.1 40. 2 100.4 12.3 150.3 335 Run Percent Efficiency Ti µmole B/Ti Al/Ti Exotherm, C Max. Solvent Total Press, Number Catalyst MM lb Ratio Ratio Temp, C mass, g psig A PE/lb Ti 10 100 1. 36 1 3 10 3.3 103. 1 1401. 3 461.50 11 75 1.82 1 3 10 3. 7 103.6 1403.8 458.50 12 50 1.71 1.5 3 10 9.3 109.6 1403.1 463.90 13 25 1.67 1.25 3 10 3. 4 103.1 1406.3 462.4 14 0 1.15 1.5 3 10 2.2 102.6 1405.1 462. 2 Run GPC GPC Mn GPC Mwl Mw2 Hi/Lo Mw Tc (onset) Tc Tg C Tm C MWDRatioC(peak)CNumberMw 10 174700 87700 1. 99-52353-10.98 5.73-40. 42 3.77 11 165500 63700 2. 6 174700 51165 4.15 12.73 7.21-41. 58 9.01 12 123800 41700 2. 97 217056 51423 3.96 14.95 9.17-41. 68 7.3 331002.842026961393900 56900 3.73 18.87 12.04 10.41 302001.88191659--21.6213.59-42.946.731456900 Run FTIR'FTIR'FTIR'FTIR'Ethylene/Density % Xtal Number Method Percent Percent Percent propylene ENBEthylenePropylene ratio 10 EPDM 67. 1 26. 2 6. 7 71. 9/28.1 0.867 10. 47 66.427.85.870.5/29.50.86510.7811EPDM 66.428.65.069.9/30.10.86511.7112EPDM 66.928.34.870.3/29.70.86613.5113EPDM 66.030.23968.6/31.40.86313.8314EPDM TABLE 1B Batch Reactor Operational Data and Physical Properties of Ethvlene/Propvlene/ENB Polvmers and Polymer Blends Tensilecommat;Elonga-I2commat;I10commat;I10/I2RunPercent Number Catalyst Break tion @ 190C/2. 16 190C/10. 1 @ 190C A (psi) Break (%) kg k 10 100 381 1988 0. 20 1. 23 6.26 11 75 445 1699 023 1. 50 6. 51 40319040.806.648.281250 13 25 438 1999 2. 42 21. 52 8.88 14 0 102 306 17. 14 102. 48 5. 98

*A- (t-butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene.

B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

-Fourier Transformation Infrared Spectroscopy.

TABLE 1C Batch Reactor Operational Data and Physical Properties of Ethvlene/Butene/ENB Polymer and Polymer Blends Run Percent Percent Butene ENB Temp, C H2 mmol Ethylene Ethylene Number Catalyst Catalyst mass, g mass, g mass, g partial A* B* pressure psig 15 100% 0% 265.5 40. 0 100 12.2 185. 6 399.7 16 75% 25% 265. 2 40. 5 100. 1 12.2 183 395.3 17 50% 50% 265. 4 40. 4 99. 4 12 183. 6 392.9 75%265.540.499.712.1182391.31825% 100%26540.2100.312.2182.4399.4190% Run Percent Efficiency Ti (immole B/ Ti Al/ Ti Ratio Exotherm, Max. Solvent Total Press, MMlbRatioCTemp,Cmass,gpsigNumberCatalyst A PE/lb Ti 1.9413104.7104.71401463.515100% 16 75% 2.96 0.75 3 10 5.7 105.8 1401. 1 463.7 17 50% 2.4 1 3 10 7.2 106. 6 1405.7 462.2 2.340.753104.31041401.44621825% 19 0% 0.96 2.5 3 10 3.6 103.9 1406. 6 467.5 Run GPC GPC Mn GPC Mwl Mw2 Hi/Lo Tc (onset) Tc (peak) Tg C Tm C Number Mw MWD Mw Ratio C C 879001.86-56773-33.1328.52-44.4743.9915163800 604002.41163800530563.0641.8833.94-44.7140.3816145300 453002.5173465514593.3844.1938.94-42.8042.6517113400 363002.33179418552003.6847.2242.81-47.0158.521884700 1955200299001. 85189163--50. 1846. 67-42. 15 62. 74 Run FTIR'FTIR'FTIR'FTIR'Ethylene/Density % Xtal Number Method Percent Percent Percent Butene ratio Ethylene Butene ENB 15 EBDM 75. 68 19. 16 5. 16 79.80/20.20 0.882 13.95 16 EBDM 75. 47 19. 89 4. 65 79.14/20.86 0.885 15.87 17 EBDM 76. 65 19. 38 3. 98 79.82/20.18 0.882 16.87 18 EBDM 76. 98 19. 75 3. 27 79.58/20.42 0.886 18.29 19 EBDM 79.31 18.18 2.52 81.35/18. 65 0.888 18. 78 TABLE 1C Batch Reactor Operational Data and Physical Properties of Ethylene/Butene/ENB Polvmer and Polymer Blends TensileElongationI2RunPercent commat; I10/I2commat;commat; Number Catalyst @ Break @, Break 190C/190C/190C A (psi) (%) 2.16 kg 10. 1 kg 15 100 1142 784 0. 19 1. 29 6. 79 16 8420.372.677.221185 11549081.037.867.631750 128812083.983147.881825 1054105216.295.35.89190 *A- (t-butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene.

B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

'Fourier Transformation Infrared Spectroscopy.

TABLE 1D Batch Reactor Operational Data and Polymer Blend Properties of Ethylene/1-Butene Polymers and Polymer Blends Run Number EB-1 EB-2 EB-3 Catalyst* A B A/B Temp, C 100. 4 100. 0 100.1 I-Butene, g 351. 4 351. 1 351. 2 Ti, umole 1. 0 0. 50 0.65 B/Ti 3. 0 3. 0 3.0 Al/Ti 10. 0 10. 0 10.0 Exotherm C 10. 2 5. 9 4.0 C2 Flow, max 22. 6 17. 6 17.3 C2 rate end 0 0 0 C2 used, g 85. 9 57. 4 52.0 Calculated Efficiency 1,794,134 132 Solvent, g 1401. 5 1406. 1 1403.2 Pressure, 452.4452.4455.1 C2 load, g 171. 8 174. 2 172.5 C2 pressure, sig 376.5 373.8 374. 5 H, mmole 6. 6 6. 4 6.6 Mw 62, 800 178, 300 137,500 Mn 32, 800 86, 500 57,300 MWD 1. 91 2. 06 2.40 -69,213Mw1- -207,262Mw2- MW Ratio Hi/Lo--2.995 12 10. 5 0. 31 0.82 I164.8 1. 83 5.45 I, o/I2 6. 17 5. 90 6.65 Density (g/cm3) 0.872 0. 866 0.868 DSC Tm Peak Melting 56.02 37.34 32. 01 % Crystallized 14. 27 11. 05 12.5 DSC Tg-51.56-53.54-54.46 Tc (onset) 46.78 30. 43 42.26 Tc (peak) 40.92 19. 1 17.78 J/g 41. 67 32. 26 36. 51

*A- (t-butylamido)dimethyl(tetramethylcyclopentadienyl)silanetit anium 1,3-pentadiene.

B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

Like the data of Table 1 A, the data reported in Tables 1 B, I C and 1 D shows that polymer blends made with a mixed catalyst system have a larger MWD than the polymers made under similar polymerization conditions with only one of the mixed catalyst components. This broaden MWD was obtained for elastomeric blends (that is, polymer blends of low density, for example, less than 0.89 g/cm3) without sacrificing, and in certain cases with an improvement to, the desirable physical properties of the polymers.

Moreover, the polymer blend components have a substantially uniform molecular architecture, at least with respect to the polymer units derived from ethylene and the a- olefin, because the reactivity ratios of Catalysts A and B were similar with respect to ethylene and the a-olefin as reported in Tables 7A-C.

Continuous Reactor Run Description Ethylene/octene compositions were prepared in a continuous reactor designed for continuous addition of reactants and continuous removal of polymer solution, devolatilization and polymer recovery. Primary catalyst 1 for all samples was (t- butylamido) dimethyl (2-methyl-s-indacen-1-ylsilanetitanium 1,3-pentadiene. Primary catalyst 2 for all samples was (t- butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene. The primary cocatalyst for all samples was trispentafluorophenyl borane. The secondary cocatalyst for all samples was triisobutyl aluminum modified methylalumoxane.

Referring to Figure 1, ethylene, octene-1, and hydrogen were combined into single stream 10 before mixed with a diluent comprising Isopar-E to form combined feed mixture stream 11 that was continuously injected into reactor 12. Primary catalyst 1, primary catalyst 2, and a blend of the primary cocatalyst and secondary cocatalyst were combined into single stream 13 which was also continuously injected into reactor 12.

Reactor exit stream 14 was continuously introduced into separator 15 in which molten polymer was continuously separated from the unreacted comonomer, unreacted ethylene, unreacted hydrogen, and solvent. Unreacted materials 16 may be recycled to the reactor by way of combined feed mixture stream 11. The molten polymer was subsequently strand chopped or pelletized (in pelletizer 17) and after being cooled, was collected (typically as pellets).

TABLE 2 Continuous Reactor Operational Date and Polymer Blend Properties Run Number 20 21 22 Pilot Plant Conditions Primary Catalyst Ratio 50/50 60/40 50/50 Primary Catalyst I * Feed (pph) 0.63 0. 85 0.62 Primary Catalyst 2* Feed (pph) 0.63 0. 56 0.62 Primary Cocatalyst Feed (pph) 0.44 0. 45 0.42 Second Cocatalyst Feed (pph) 0.43 0. 52 0.48 Primary Catalyst I Conc. (ppm) 10 10 10 Primary Catalyst 2 Conc. (ppm) 10 11 10 Primary Cocatalyst Conc. (ppm) 1250 1404 1250 Secondary Cocatalyst Conc. (ppm) 125 125 125 Primary Cocatalyst molar ratio 4. 0 4. 9 3.91 Second Cocatalyst molar ratio 7. 36 9. 6 8.4 Reactor temperature (C) 80.9 81. 3 88.9 Reactor Pressure (psi) 476.5 469. 1 474.3 Ethylene Feed (pph) 30.1 30. 3 29.0 Octene Feed (pph) 35.1 36. 2 28.9 Ethylene Conversion (%) 78.7 81. 0 82.7 Solvent flow (pph) 359.6 379. 9 243 Solids (%) 9.8 9. 9 13.1 Production Rate (pph) 39.5 42. 0 37.6 Product Properties Mooney 49. 9 54. 7 33.1 Mwl (weight ave. mol. wt.) 262976 267269 208088 Mw2 (weight ave. mol. wt.) 88310 90245 70390 Mwl/Mw2 2. 98 2. 96 2.96 Overall Mw (weight ave. mol. wt.) 183377 188425 148463 Mw/Mn 2.83 2. 75 2.76 190C Viscosity @ 0. 1 rad/sec 453300 568590 289730 190C Viscosity @ 100 rad/sec 27837 31714 22092 Rheology ratio (0.1/100) 16.28 17. 93 13.11 Density (g/cm3) 0.8657 0. 8675 0.8705 DSC peak cooling point (C) 38.85 40. 76 45.69 DSC peak melting point (C) 52.89 56. 25 54.98

Table 2 shows the ratio of primary catalyst 1 to primary catalyst 2, primary catalysts 1 and 2 feed in pounds per hour (pph), primary and secondary cocatalyst feeds in pph, catalyst component concentrations in parts per million parts of metal (ppm), catalyst molar ratios of cocatalyst metal species (B or AI) to total metal (Ti) concentration in the catalyst, reactor temperature in degrees Centigrade, reactor pressure in psi, solvent flow rates in pph, and ethylene (C2) and octene (C8) in pph. Table 2 also shows the percent conversion of ethylene, percent polymer or solids in the reactor, polymer production rate in pph, and polymer properties (Mooney, molecular weight, rheology, density and DSC data). Hydrogen was not used in these runs.

The data reported in Table 2 clearly demonstrate that the mixed catalyst systems produce broad MWD polymer blends in an efficient and facile manner. This was illustrated further by the viscosity shear rate curve at 190 C of Figure 2, and the Gottfert Rheotens data of Figure 3.

Figure 2 shows a 190 C viscosity versus frequency (rad/sec) relationship for two polymers and one polymer blend each of about 30 Mooney viscosity measured at 125 C.

One of the polymers was produced using primary catalyst 1, and the other was produced using primary catalyst 2. Both of these polymers were of a narrower MWD (about 2.0) as compared to the polymer blend produced using a mix of primary catalysts I and 2 (that is, a mixed CGC system). Since the mixed CGC system produced a polymer blend with a broader MWD than either of the blend components, Figure 2 reports a higher shear thinning behavior (that is, the rate of change in viscosity at different shear rates). This means that the polymer blend will process through fabrication equipment better (for example, more will process through a given piece of equipment per unit of time at fixed conditions) than its individual components.

Figure 3 also reports the comparison between two products having about 30 Mooney viscosity. One of the two products was made using primary catalyst 1, and the second was made using a mixed CGC system of which one of the components was primary catalyst 1. In spite of the two polymers having similar a Mooney viscosity, the maximum melt strength (force) of the polymer blend prepared using the mixed CGC system was 10 cN versus 7 cN for the polymer prepared using primary catalyst l. This figure demonstrates that the polymer blend produced using a mixed CGC system has higher melt strength as compared to a polymer of similar Mooney viscosity made with only one component of the system. Such polymer blends exhibit better processing

properties for applications requiring higher melt (or green) strength, for example, calendering, blow molding and thermoforming.

Moreover, the polymer blend components have a substantially uniform molecular architecture as evidenced by the single DSC melting and cooling points (the melting peak tends to be broader at the lower densities). Again, this was consistent with the similarity in reactivity ratios of catalysts A and B with respect to ethylene and 1-octene as reported in Table 7A.

Crosslinkin Data Primary catalyst 1 for all samples was (t-butylamido) dimethyl (2-methyl-s-indacen- I-yl) silanetitanium 1,3-pentadiene. Primary catalyst 2 for all samples was (t- butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene.

The crosslinked elastomers identified in Table 3 below were prepared by melt blending the polymer blend of Run 22 (reported in Table 2) at 90 C in a Haake rheometer equipped with a 310 cc mixing bowl and Banbury style rotors. The peroxide was added to the polymer melt and mixed at 40 rpm for 2-3 minutes. The blended compositions were removed from the Haake bowl and used to produce compression-molded plaques.

The plaques were compression molded and crosslinked at 177 C for T90 plus 2 minutes to ensure full cure. Plaques were removed and immersed in a water bath until cool per ASTM D-3182. ASTM test samples were then cut from the plaques for testing.

The results were also reported in Table 3 and as was evident from these results, the plaques made with the mixed catalyst system exhibit comparable to better physical properties than the plaques made from one of the catalyst components alone. Enhanced properties include those of tear strength, tensile (break and yield) and trouser tear.

TABLE 3 Physical Properties of Crosslinked Ethvlene/1-Octene 30 Mooney Elastomers Sample Number 23 24 25 26 27 28 29 30 31 Primary Catal st 2* Prima Catal st 1 * Dual Catal st* DICUP ADDITION 1.5 2.5 3.5 1.5 2.5 3.5 1.5 2.5 3.5 (pph) POLYMER weigh-up 200 200 200 200 200 200 200 200 200 PEROXIDE weigh-up 3 5 7 3 5 7 3 5 7 Shore A Hardness ASTM D-2240 I second 67.6 67.5 66.8 68.8 68.4 67.7 72.6 70.8 71.4 10 second 65. 2 65.0 64.3 66. 3 65.9 65.4 70.3 68.6 69.1 Density ASTM D-792 at 23° 0. 870 0.871 0.871 0.871 0.870 0.871 0.871 0.872 0.873 Tensile @ 20 in./min ASTM D-638 Tensile @ Break (psi) 872 597 502 953 650 543 993 759 566 Ult. Elongation (%) 582 444 357 624 460 378 588 447 332 Tensile Yield (psi) 172 158 162 190 158 140 224 185 192 Elon Yield (%) 29 27 28 31 24 20 34 26 28 Young's Modulus (psi) 872 940 939 799 962 1014 910 1097 1191 Toughness (Ibs-in.) 83 54 39 99 60 45 96 67 45 100% Modulus (psi) 289 286 291 305 306 310 336 340 341 Type C Tear ASTM D- 624 1 Tear Strength (pli) 187.90 163.60 134.00 184. 30 177.90 147.60 214.50 194.70 177.30 Total Energy (in.-lbs) 57.72 37.12 21.52 53.94 45.12 22.43 64.92 42.75 29.13 Trouser Tear ASTM D- 624 Tear Strength (pli) 22.40 18.30 12.40 28.90 14.20 11.60 35.20 22.00 14.70 Total Energy (in.-lbs) 11.37 9.11 3.95 13.60 5.37 4.37 19.48 8. 33 3.91 ODR@ 177 C ASTM D-2084 Min Torque 9.40 10. 22 10.34 8.96 9.70 10.96 11.47 10.64 11.36 Max Torque 60.03 68.20 79.12 57.83 71.71 79.24 72.08 73.85 82.09 Delta 50.63 57.98 68.78 48.87 62.01 68.28 60.61 63.21 70.73 T2 0.49 0.57 0.43 1.04 1. 01 0.52 1.04 0.48 0.57 T90 5.09 5.09 4. 35 5.35 5.08 4.44 4.56 4. 35 4.33

Thermoplastic Olefin (TPO) Applications The polymer blends identified in Table 4 were mixed in the reported ratios, and then tumble blended in a 5-gallon bucket to assure good dispersion of all ingredients. The polymer blends were then melt blended in a ZSK 30 millimeter Werner Pfleiderer, corotating, twin-screw extruder equipped with a screw configuration that had basic kneading blocks followed by gear mixer flights to produce a medium shear, high mixing configuration. The extruder operated at a melt temperature of approximately 240 C and a speed of 200 rpm. The melt blends were passed through a 100 F water bath, chopped into granules, and collected for injection molding.

TABLE 4 TPO Formulations of Elastomers Made With a Mixed Catalyst Svstem Sample Number 32 33 34 35 36 37 Accpro 9934*' (35 melt index) 70 70---- Profax 6323*2 70 63 70 63 Run 22 Polymer Blend 30-30 27-- (33 Mooney) Run 20 Polymer Blend-30--30 27 (52 Mooney) AG 101 talc*3 10 10 Irganox 1076*'0.2 0.2 0.2 0.2 0. 2 0.2 *'Propylene homopolymer having a density of 0.90 g/cc and b of 35 g/10 min at 230 C, available from Amoco.

*2Propylene homopolymer having a density of 0.90 g/cc and b of 12 g/10 min at 230 C, available from Montel.

*3Available from Microtuff Specialty Minerals *4Phenolic antioxidant available from Ciba Specialty Chemicals.

ASTM samples were prepared by injection molding on a Arburg Model 370C- 800-225 (800 kilonewton (kN) hydraulic clamping force) reciprocating screw injection molding machine. Molding temperatures for the barrel were set at 250 F (feed), 385,430, 440 and 430 F (barrel through nozzle) while the mold temperature was 88 F. Injection cycles were approximately 1.75 seconds injection, 30 seconds holding and 20 seconds cooling. The hold pressures were approximately 600 bars and the velocities and pressures were adjusted as needed to completely fill mold cavities.

ASTM standard procedures were used to evaluate the molded samples. In addition, notched Izod values were obtained using an Izod impact tester and a low speed notcher equipped with a 10 mil (0.25 mm) wheel in accordance with ASTM D-256.

Unnotched weldline Izod samples were cut from the middle of a double gated tensile bar and tested on the lzod impact tester. Test results were reported in Table 5. The Izod impact values were measured in units of foot-pounds per square inch (fpsi). Tensile strengths were measured in units of pounds per square inch (psi).

TABLE 5 Physical Properties of TPO Formulations of Elastomers Made With a Mixed Catalyst System Sample Number 32 33 34 35 36 37 Shore D Hardness ASTM D-2240 1 second66.9 66.3 61.6 64.5 63.8 65.4 10 second 643 63.7 58.1 61.2 60.8 62.3 Tensile Cd. w in./min ASTM D-6382 Tensile commat; Break (psi) 2878 2542 2790 2583 3259 2665 Ult. Elongation (%) 25 65 577 351 534 194 Tensile Yield (psi) 3267 2972 2718 2495 2861 3242 Elong @ Yield (%) 4 5 14 7 8 6 Rheomet (d/10 min) ASTM D-1238 I2 commat; 230 C/2.16 kg 14. 4 10.7 5.9 5.6 5.7 4.5 Weld Line @ 2 in./min ASTM D-638 Tensile @ Break (psi) 2139 2568 1984 1915 2370 2088 Ult. Elongation (%) 1 3 3 1 8 3 Tensile @ Yield (psi) 2131 2562 1982 1912 2406 2079 Elong @ Yield (psi) 3 3 1 6 2 3-Point Flex ASTM D-790 Flex Modulus (psi) 168900 155576 102315 170010 112305 172583 2% Secant Modulus (psi) 154042 142289 93316 137421 103310 141590 Gloss ASTM D-523 20° 35.1 16.8 67.8 45.9 27.5 36.3 60° 51.2 30.9 82.3 68.9 66.6 67.6 85° 84.3 79.1 98.8 95.3 92.1 91.5 Dynacup Total Ener (ft lb) 23C 27.9 27.7 26 27.2 31 32. 3 -30 C 26.6 25.9 39.4 24.5 36.1 17.0 Izod Impact Strength (ft Ibs/in.) 23 C 1. 54 1.64 14.39 12.03 13.89 12. 3 0 C 1.48 1.16 9.93 5. 34 1.85 2. 25 RT Weldline Izods (ft lbs/in.) 23 C 1. 74 3.95 5.85 2.56 7.66 2.49 Heat Distortion @ 66 psi HDT in C 99.5 91.7 80.3 78.9 77.5 81.2

The data reported in Table 5 shows a unique balance of rheometry, modulus, impact strength, and weld line strength important for TPO automotive applications.

Blend of TPO and a Medium Mooney Viscosity Ethylene/1-Octene Polvmer Blend Medium Mooney viscosity, for example, 35-55, polymer blends of ethylene and 1- octene (that is, an ethylene/1-octene copolymer made with a mixed CGC system and of substantially uniform molecular architecture) yield a superior combination of tensile strength, toughness, scuff or abrasion resistance, color stability and thermoformability than that obtainable either with a medium Mooney viscosity EPDM or a low Mooney viscosity, for example, less than 35, conventional ethylene/1-octene copolymer (that is, a nonblended copolymer) when blended with a TPO. Such TPO blends were useful in many thermoforming operations, for example, the manufacture of automotive instrument panel skins.

The following TPO blends were mixed in a Haake 230 cm3 mixing bowl fitted with roller blades: TABLE 6A TPO Blends Blend 38 38-C I 38-C2 Profax6323 25 25 25 Surlyn9520 27 27 27 ElvaloyAS 3 3 3 Nordel3681 0 45 0 ENGAGE8150 0 0 45 EOPolymer Blend 45 0 0 Profax 6323, available from Montel, was a propylene homopolymer having a density of 0.90 g/cc and a melt flow index of 12 grams/10 min. at 230°C. Surlyn 9520, available from DuPont, was an ethylene/methacrylic acid copolymer partially neutralized with zinc, having a melt index of 1.1 and a specific gravity of 0.95 g/cc. Elvaloy AS, also supplied by DuPont, was an ethylene/n-butyl acrylate/glycidyl methacrylate copolymer with a melt index of 12 g/10 min and a specific gravity of 0.94 g/cc. Nordel 3681, produced by DuPont Dow Elastomers, L. L. C., was an ethylene/propylene/diene terpolymer using 1,4 hexadiene as the diene termonomer, having 71 wt. percent ethylene with a nominal 52 ML (1+4) Mooney viscosity and was polymerized via a vanadium based catalyst.

ENGAGE 8150 was an ethylene/1-octene copolymer with a density of 0.868 g/cc, a

nominal melt index of 0.5 g/10 min at 190°C, and a nominal Mooney viscosity of 45 ML (1+4). It was polymerized with t-butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene. EO polymer blend was an ethylene/1-octene copolymer with a density of 0.868 g/cc and a nominal Mooney viscosity of 45 ML (1+4), and it was polymerized via a 50/50 wt./wt. ratio of t- butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene and t- butlyamido) dimethyl (2-methyl-s-undacen-1-yl) silanetitanium 1,3-pentadiene. Meltindex was measured in accordance with ASTM D1238. Mooney viscosity was measured in accordance with ASTM D 1646.

The following mix procedure was used: 1) Set Haake bowl to 190 C, split signal from melt thermocouple to control Thermocouple for bowl.

2) Start initially at 30 rpm, add all polymers, except for Elvaloy AS, to bowl.

3) Increase speed to 75 rpm 4) Mix for five minutes, then add Elvaloy AS and mix for four minutes.

5) Remove melt from bowl and press out into crude plaques using a 32 mm thick Mold at 190 C for three minutes at 18,200 Kg pressure, then cool for three Minutes at 18,200 Kg pressure.

The samples were then compression molded into 15.2 cm x 25.5 cm x 1.5 mm thick plaques using the following compression cycle: 1) 3 minutes preheat at 210 C, no pressure.

2) 3 minutes at 18,200 Kg, 210 C.

3) 3 minutes at 18,200 Kg, cooling.

Sample hardness was tested according to ASTM D 2240. Tensile properties were tested according to ASTM D 638. Tear properties were tested in accordance with ASTM D 624.

Abrasion resistance was measured according to ASTM D 1630.

Elevated temperature stress-strain measurements give an indication of how the compound with thermoform at elevated temperature. During sheet thermoforming, the compound must exhibit optimum stress-strain behavior. A very stiff product will not yield under vacuum. On the other hand, the sheet at the forming temperature must exhibit enough stress response to minimize thin spots during the forming operation. Tensile properties at 140 C were measured by cutting tensile samples from an ISO T2 die. These

samples were placed in a tensile tester fitted with an environmental chamber heated to 140 C. The tensile samples were strained at a rate of 50 cm/min. Strain was measured via an optical extensiometer.

TABLE 6B TPV Blend Properties 38-C1Property38 38-C2 ShoreD Hardness 38.342.845.0 1 second Tensile commat; 7.9 cm/min 12.28.9 Tensile commat; Break (Mpa) 12.28.9 Ult. Elongation (%) 435 262 486 Type C Tear 398 295 374 TearStrength (PLI) NBSAbrasion 71 58 49 Index Hot Stress-strain @ 140 C 0306 0354 0. 235 Max Eng. Stress, Mpa True Stress 500% elong., Mpa 1.78 1.88 1.38 As can be seen from the results reported in Table 6B, Comparative Example 38-C1, which contains Nordel 3681, contains lower ultimate tensile and elongation than either Comparative Example 38-C2 or Example 38, both containing ethylene/1-octene copolymers. However, Comparative Example 38-CI exhibits acceptable stress-strain characteristics at 140 C. Note that Example 38 exhibits tensile stress at 140 C much closer to Comparative Example 38-C1 than does Comparative Example 38-C2. Example 38 was much more suitable for vacuum thermoforming than Comparative Example 38- C2. Further, note that Example 38 exhibits significantly higher abrasion resistance than either of the two comparative examples. Thus, Example 38 exhibits a unique combination of high ultimate tensile strength, elongation, abrasion resistance and high elevated temperature tensile stress, making it especially suitable for automotive interior.

Tape Extrusion Comparison A 30 Mooney polymer produced with catalyst A ( (t-butylamido) dimethyl- (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene) was compared to a 30 Mooney polymer produced with a mixed catalyst A + catalyst B ( (t- butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene) in a extruded tape test. Both polymers were extruded on a 2*4 inch 30/1 L/D Killion extruder

having a barrier ET screw. Dimensions of the tape die were 1.5 inches wide and 0.06 inches thick. The extruder temperature profile was: feed 100°C, 176°C, 204°C, 204°C, 204°C, and 204°C at the die. The extruder was run at 35 rpm and 35 pounds per hour.

Results from this test indicated sever melt fracture on the tape made with the polymer produced by catalyst A while the tape made from the polymer produced by the mixed catalyst system of A and B showed no evidence of melt fracture.

Reactivitv Ratios Reactivity ratios for propylene, butene, 1-octene and ENB were reported in Tables 7A-C. These ratios were based on the data reported for runs 1,3,4,6-8,10,14-15 and 19.

All the values assumed r2 was equal to 0.5.

TABLE 7A Ethvlene/Octene Copolvmer Run Catalyst Reactor Polymer Composition C wt% Cs Wt % rl value I A 90 64. 59 35. 41 3.5 3 B 90 65. 17 34.83 3.6 4 A 110 64.91 35.09 5.1 6 B 110 58.40 41.60 3.8 7 B 110 45.50 54.50 3.3 8chu76.00 24.00 14.3

*A- (t-butylamido) dimethyl (tetramethylcyclopentadienyl) silanetitanium 1,3-pentadiene.

B- (t-butylamido) dimethyl (2-methyl-s-indacen-1-yl) silanetitanium 1,3-pentadiene.

C- [N- (1, I-dimethylethyl)-1, I-dimethyl-1- ( (1,2,3,3a, 7a-h)-3-(1-pyrrolidinyl)-l H-inden- 1-yl) silanaminato- (2-)-N] [(2, 3,4,5,-h)-2,4-pentadiene)]-titanium.

As reported in Table 7A, the reactivity ratios for catalysts A and B were essentially the same, that is, within 5 percent, for ethylene/1-octene polymerization at 90 C. At the higher temperature of 110 C, the reactivity ratios were still similar, for example, within 35 percent. The reactivity ratios for catalysts B and C at 1 10 C were, in contrast, very different with the reactivity ratio for catalyst C 4.33 times greater than that of catalyst B. The large difference in reactivity ratio was evident in the fact that polymerization with catalyst C yielded a polymer with less than half the amount of 1- octene incorporated into it as was incorporated into it with catalyst B.

TABLE 7B <BR> <BR> EPDM Terpolymers Composition Run Catalyst C, wt % C3 Wt % ENB Wt % ri value for C3 rl value for Number Code ENB 14 A 66 30.2 3.9 2.8 5.5 10 B 67.1 26.2 6.7 3.5 3.6

As reported in Table 7B, the reactivity ratios for ethylene/propylene polymerization at 100 C were similar for catalysts A and B, that is, within 25 percent of each other. The reactivity ratios for ethylene/ENB, in contrast, were further apart, that is, 52 percent.

TABLE 7C EBDM Terpolvmers Composition Run Catalyst Cv wt % C4 Wt % ENB Wt % rl value for C4 rl value for Number Code ENB 19 A 79. 31 18.18 2.52 7.3 8.7 15 B 75.68 19.16 5.16 6.4 4.2

As reported in Table7C, the reactivity ratios for ethylene/butene polymerization at 100 C with catalysts A and B were very similar, with 14 percent of one another. In contrast, the reactivity ratios for ethylene/ENB at 100 C with catalysts A and B were very different, with the reactivity ratio of catalyst A more than twice that of catalyst B.

For comparative purposes, Kaminsky and Schlobohm report in Makromol. Chem., Makromol. Svmp., that the reactivity ratio rl of bis (cyclopentadienyl) zirconium dichloride (a sandwich type zirconium compound) for ethylene polymerization with butene at 85 C was 125, more than 17 times that of catalyst A at 100 C.

Although the invention has been described in considerable detail through the specification and examples, one skilled in the art can make many variations and modifications without departing from the spirit and scope of the invention as described in the following claims.