CROSS REFERENCE TO RELATED APPLICATIONS

This invention is a continuation in part of U.S. Ser. No. 15/869,906, filed Jan. 12, 2018 which claims priority to and the benefit of to U.S. Ser. No. 62/464,939, filed Feb. 28, 2017. This application also relates to U.S. Ser. No. 62/212,405, filed Aug. 31, 2017; U.S. Ser. No. 62/332,940, filed May 6, 2016; U.S. Ser. No. 62/332,921, filed May 6, 2016; U.S. Ser. No. 62/357,033, filed Jun. 30, 2016; and U.S. Ser. No. 15/629,586, filed Jun. 21, 2017.

FIELD OF THE INVENTION

This invention relates to the use of quinolinyldiamido transition metal complexes and catalyst systems with an activator and a metal hydrocarbenyl chain transfer agent, such as an aluminum vinyl-transfer agent (AVTA), to produce branched ethylene-propylene-diene terpolymers.

BACKGROUND OF THE INVENTION

Pyridyldiamido transition metal complexes are disclosed in US 2015/0141601; US 2014/0316089; US 2012/0071616; US 2011/0301310; US 2011/0224391; and US 2010/0022726, where such complexes are useful as catalyst components for the polymerization of olefins.

US 2015/0141596; US 2015/0141590; and US 2014/0256893 describe the production of polyolefins using pyridyldiamido catalysts in the presence of chain-transfer agents that do not feature transferrable vinyl groups.

Macromolecules 2002, 35, 6760-6762 discloses propene polymerization with tetrakis(pentafluorophenyl)borate, 7-octenyldiisobutylaluminum, and racMe₂Si(2-Me-indenyl)₂ZrCl₂or Ph₂C(cyclopentadienyl)(fluorenyl)ZrCl₂to produce polypropylene with octenyldiisobutylaluminum incorporated as a comonomer.

Japanese Kokai Tokyo Koho (2004), JP 2004-83773-A describes the preparation of polypropylene in the presence of trialkenylaluminum using metallocene and Ziegler-Natta catalysts.

Macromolecules 1995, 28, 437-443 describes the formation of isotactic polypropylene containing vinyl end groups by the Ziegler-Natta catalyzed polymerization of propylene in the presence of dialkenylzincs.

Macromolecules 2002, 35, 3838-3843 describes the formation of long-chain branched polypropylene via the insertion of in situ formed vinyl-terminated polypropylene into growing polymer chains.

Macromolecules 2002, 35, 9586-9594 describes the formation of long-chain branched copolymers of ethylene and alpha olefins via the insertion of in situ formed vinyl-terminated polymer into growing polymer chains.

Eur. Pat. Appl. (2012), EP 2436703 A1 describes the production of comb architecture branch block copolymers in a process that uses dual catalysts and a zinc-based polymerizable chain shuttling agent.

WO 2007/035492 describes the production of long-chain branched and branch block copolymers by polymerization of alkene monomers in the presence of a zinc-based polymerizable shuttling agent.

WO 2016/102690 discloses a process for preparation of a branched polyolefin using a metal hydrocarbyl transfer agent.

References of interest also include: 1) Vaughan, A; Davis, D. S.; Hagadorn, J. R. in Comprehensive Polymer Science, Vol. 3, Chapter 20, “Industrial catalysts for alkene polymerization”; 2) Gibson, V. C.; Spitzmesser, S. K. Chem. Rev. 2003, 103, 283; and 3) Britovsek, G. J. P.; Gibson, V. C.; Wass, D. F. Angew. Chem. Int. Ed. 1999, 38, 428; 4) US 2002/0142912; 5) U.S. Pat. No. 6,900,321; 6) U.S. Pat. No. 6,103,657; 7) WO 2005/095469; 8) US 2004/0220050A1; 9) WO 2007/067965; 10) Froese, R. D. J. et al., J. Am. Chem. Soc. 2007, 129, pp. 7831-7840; 11) WO 2010/037059; 12) US 2010/0227990 A1; 13) WO 2002/38628 A2; 14) US 2014/0256893; 15) Guerin, F.; McConville, D. H.; Vittal, J. J., Organometallics, 1996, 15, p. 5586.

There is still a need in the art for new and improved catalyst systems for the polymerization of ethylene, propylene and diene monomers, in order to achieve specific polymer properties, such as increased branching, high molecular weight, to increase conversion or comonomer incorporation, and to develop branch-on-branch structures for foaming processability.

SUMMARY OF THE INVENTION

This invention relates to processes to produce branched ethylene-propylene-diene terpolymers comprising:

1) contacting monomers comprising propylene, ethylene and diene with a catalyst system comprising an activator, a metal hydrocarbenyl chain transfer agent (such as an aluminum vinyl transfer agent), and one or more single site catalyst complexes, such as quinolinyldiamido complexes represented by the Formula I or II;

[Image Omitted]

wherein:

M is a Group 3, 4, 5, 6, 7, 8, 9, or 10 metal;

E is C, Si or Ge;

X is an anionic leaving group;

L is a neutral Lewis base;

R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups;

R², R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are each independently selected from the group consisting of hydrogen, hydrocarbyls, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyls, halogen, and phosphino;

J is a divalent group that forms a three-atom-length bridge between the pyridine ring and the amido nitrogen;

n is 1 or 2;

m is 0, 1, or 2;

two X groups may be joined together to form a dianionic group;

two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group;

adjacent groups from the following R², R³, R4, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²may be joined to form a ring; and

2) obtaining branched ethylene-propylene-diene terpolymers comprising from about 98.9 to 30 wt % propylene, from 1 to 70 wt % ethylene, from 0.1 to 20 wt % diene monomer, and a remnant of the metal hydrocarbenyl chain transfer agent, wherein said branched propylene copolymer: a) has a g′_visof less than 0.90; b) preferably, is essentially gel free (such as 5 wt % or less of xylene insoluble material); c) has an Mw of 250,000 g/mol or more; d) has a Mw/Mn of greater than 3.0; and e) has an Mz of 850,000 g/mol or more,

wherein the process preferably has a diene conversion of at least 15% and the ratio of a metal hydrocarbenyl chain transfer agent (such as an aluminum vinyl transfer agent) to the one or more single site catalyst complexes is at least 100:1.

This invention also relates to processes where the metal hydrocarbenyl chain transfer agent in the above catalyst systems is one or more aluminum vinyl transfer agents (AVTA) represented by formula:

Al(R′)_3-v(R″)_v

wherein each R′, independently, is a C₁-C₃₀hydrocarbyl group; each R″, independently, is a C₄-C₂₀hydrocarbenyl group having an end-vinyl group; and v is from 0.1 to 3.

This invention further relates to novel branched ethylene-propylene-diene terpolymers comprising from about 98.9 to 30 wt % propylene, from 1 to 70 wt % ethylene, from 0.1 to 20 wt % diene monomer, and a remnant of the metal hydrocarbenyl chain transfer agent, wherein said branched propylene copolymer: a) has a g′_visof less than 0.90; b) is essentially gel free (such as 5 wt % or less of xylene insoluble material); c) has an Mw of 250,000 g/mol or more; d) has a Mw/Mn of 3.0 or more; and e) has an Mz of 850,000 g/mol or more.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a drawing of the reaction of iBu₂AlH and 1,7 octadiene at various conditions. Compounds 1 and 2 represent average compositions as hydrocarbyl and hydrocarbenyl groups may exchange between Al centers. Triene product 3 may be a mixture of similar molecules containing a vinylidene group.

FIG. 2 is a plot of Frequency dependent loss tangent values of EPDM11 and EPDM20 from the Experimental section compared to comparative EPDMA and EPDMB.

FIG. 3 is a reduced van Gurp-Palmen plot of EPDM11 and EPDM20 from the Experimental section compared to comparative EPDMA and EPDMB.

DETAILED DESCRIPTION OF THE INVENTION
Definitions

This invention relates processes to produce ethylene-propylene-diene terpolymers using transition metal complexes and catalyst systems that include the transition metal complexes. The term complex is used to describe molecules in which an ancillary ligand is coordinated to a central transition metal atom. The ligand is bulky and stably bonded to the transition metal so as to maintain its influence during use of the catalyst, such as polymerization. The ligand may be coordinated to the transition metal by covalent bond and/or electron donation coordination or intermediate bonds. The transition metal complexes are generally subjected to activation to perform their polymerization or oligomerization function using an activator which is believed to create a cation as a result of the removal of an anionic group, often referred to as a leaving group, from the transition metal.

As used herein, the numbering scheme for the Periodic Table groups is the new notation as set out in Chemical and Engineering News, 63(5), 27 (1985).

“Catalyst productivity” is a measure of how many grams of polymer (P) are produced using a polymerization catalyst comprising W g of catalyst (cat), over a period of time of T hours; and may be expressed by the following formula: P/(T×W) and expressed in units of gPgcat⁻¹hr⁻¹. Conversion is the amount of monomer that is converted to polymer product, and is reported as mol % and is calculated based on the polymer yield and the amount of monomer fed into the reactor. Catalyst activity is a measure of how active the catalyst is and is reported as the mass of product polymer (P) produced per mole of catalyst (cat) used (kgP/molcat).

An “olefin,” alternatively referred to as “alkene,” is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond. For purposes of this specification and the claims appended thereto, when a polymer or copolymer is referred to as comprising an olefin, the olefin present in such polymer or copolymer is the polymerized form of the olefin. For example, when a copolymer is said to have an “ethylene” content of 35 wt % to 55 wt %, it is understood that the mer unit in the copolymer is derived from ethylene in the polymerization reaction and said derived units are present at 35 wt % to 55 wt %, based upon the weight of the copolymer. A “polymer” has two or more of the same or different mer units. A “homopolymer” is a polymer having mer units that are the same. A “copolymer” is a polymer having two or more mer units that are different from each other. A “terpolymer” is a polymer having three or more mer units that are different from each other. “Different” as used to refer to mer units indicates that the mer units differ from each other by at least one atom or are different isomerically. Accordingly, the definition of copolymer, as used herein, includes terpolymers and the like. An oligomer is typically a polymer having a low molecular weight, such as an Mn of less than 25,000 g/mol, or in an embodiment less than 2,500 g/mol, or a low number of mer units, such as 75 mer units or less or 50 mer units or less. An “ethylene polymer” or “ethylene copolymer” is a polymer or copolymer comprising at least 50 mol % ethylene derived units, a “propylene polymer” or “propylene copolymer” is a polymer or copolymer comprising at least 50 mol % propylene derived units, and so on. An ethylene-propylene-diene terpolymer (“EPDM”) is defined to be a terpolymer comprising ethylene, propylene and diene monomers, preferably comprising from 98.9 to 30 wt % propylene, from 1 to 70 wt % ethylene, from 0.1 to 20 wt % diene monomer.

For the purposes of this invention, ethylene shall be considered an α-olefin.

For purposes of this invention and the claims thereto, when a polymer is referred to as comprising a metal hydrocarbenyl chain transfer agent, the metal hydrocarbenyl chain transfer agent present in such polymer or copolymer is the polymerized portion of the metal hydrocarbenyl chain transfer agent, also referred to as the remnant of the metal hydrocarbenyl chain transfer agent. The remnant of a metal hydrocarbenyl chain transfer agent is defined to be the portion of the metal hydrocarbenyl chain transfer agent containing an allyl chain end that becomes incorporated into the polymer backbone. For example if the allyl chain end of the metal hydrocarbenyl chain transfer agent is CH₂═CH—(CH₂)₆, the sp²carbons of the metal hydrocarbenyl chain transfer agent become a part of the polymer backbone and the —(CH₂)₆, becomes a part of a side chain.

For purposes of this invention and claims thereto, the term “substituted” means that a hydrogen group has been replaced with a heteroatom, or a heteroatom-containing group. For example, a “substituted hydrocarbyl” is a radical made of carbon and hydrogen where at least one hydrogen is replaced by a heteroatom or heteroatom-containing group.

A metallocene catalyst is defined as an organometallic compound with at least one π-bound cyclopentadienyl moiety (or substituted cyclopentadienyl moiety) and more frequently two π-bound cyclopentadienyl moieties or substituted cyclopentadienyl moieties.

As used herein, M_nis number average molecular weight, M_wis weight average molecular weight, and M_zis z average molecular weight, wt % is weight percent, and mol % is mole percent. Molecular weight distribution (MWD), also referred to as polydispersity index (PDI), is defined to be M_wdivided by M_n. Unless otherwise noted, all molecular weight units (e.g., M_w, M_n, M_z) are g/mol.

Unless otherwise noted all melting points (Tm) are DSC second melt.

The following abbreviations may be used herein: dme is 1,2-dimethoxyethane, Me is methyl, Ph is phenyl, Et is ethyl, Pr is propyl, iPr is isopropyl, n-Pr is normal propyl, Bu is butyl, cPR is cyclopropyl, iBu is isobutyl, tBu is tertiary butyl, p-tBu is para-tertiary butyl, nBu is normal butyl, sBu is sec-butyl, TMS is trimethylsilyl, TIBAL is triisobutylaluminum, TNOAL is tri(n-octyl)aluminum, MAO is methylalumoxane, p-Me is para-methyl, Ph is phenyl, Bn is benzyl (i.e., CH₂Ph), THF (also referred to as thf) is tetrahydrofuran, RT is room temperature (and is 23° C. unless otherwise indicated), tol is toluene, EtOAc is ethyl acetate, Cy is cyclohexyl and AVTA is an aluminum-based vinyl transfer agent.

A “catalyst system” comprises at least one catalyst compound and at least one activator. When “catalyst system” is used to describe such the catalyst compound/activator combination before activation, it means the unactivated catalyst complex (pre-catalyst) together with an activator and, optionally, a co-activator. When it is used to describe the combination after activation, it means the activated complex and the activator or other charge-balancing moiety. The transition metal compound may be neutral as in a pre-catalyst, or a charged species with a counter ion as in an activated catalyst system. For the purposes of this invention and the claims thereto, when catalyst systems are described as comprising neutral stable forms of the components, it is well understood by one of ordinary skill in the art, that the ionic form of the component is the form that reacts with the monomers to produce polymers.

In the description herein, the catalyst may be described as a catalyst precursor, pre-catalyst compound, catalyst compound, transition metal complex, or transition metal compound, and these terms are used interchangeably. A polymerization catalyst system is a catalyst system that can polymerize monomers to polymer. An “anionic ligand” is a negatively charged ligand which donates one or more pairs of electrons to a metal ion. A “neutral donor ligand” is a neutrally charged ligand which donates one or more pairs of electrons to a metal ion. Activator and cocatalyst are also used interchangeably.

A scavenger is a compound that is typically added to facilitate polymerization by scavenging impurities. Some scavengers may also act as activators and may be referred to as co-activators. A co-activator, that is not a scavenger, may also be used in conjunction with an activator in order to form an active catalyst. In some embodiments a co-activator can be pre-mixed with the transition metal compound to form an alkylated transition metal compound.

Non-coordinating anion (NCA) is defined to mean an anion either that does not coordinate to the catalyst metal cation or that does coordinate to the metal cation, but only weakly. The term NCA is also defined to include multicomponent NCA-containing activators, such as N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, that contain an acidic cationic group and the non-coordinating anion. The term NCA is also defined to include neutral Lewis acids, such as tris(pentafluorophenyl)boron, that can react with a catalyst to form an activated species by abstraction of an anionic group. An NCA coordinates weakly enough that a neutral Lewis base, such as an olefinically or acetylenically unsaturated monomer can displace it from the catalyst center. Any metal or metalloid that can form a compatible, weakly coordinating complex may be used or contained in the noncoordinating anion. Suitable metals include, but are not limited to, aluminum, gold, and platinum. Suitable metalloids include, but are not limited to, boron, aluminum, phosphorus, and silicon. Activators containing non-coordinating anions can also be referred to as stoichiometric activators. A stoichiometric activator can be either neutral or ionic. The terms ionic activator and stoichiometric ionic activator can be used interchangeably. Likewise, the terms neutral stoichiometric activator and Lewis acid activator can be used interchangeably. The term non-coordinating anion activator includes neutral stoichiometric activators, ionic stoichiometric activators, ionic activators, and Lewis acid activators.

For purposes of this invention and claims thereto in relation to catalyst compounds, the term “substituted” means that a hydrogen group has been replaced with a hydrocarbyl group, a heteroatom, or a heteroatom-containing group. For example, methyl cyclopentadiene (Cp) is a Cp group substituted with a methyl group.

The terms “hydrocarbyl radical,” “hydrocarbyl,” “hydrocarbyl group,” “alkyl radical,” and “alkyl” are used interchangeably throughout this document. Likewise, the terms “group,” “radical,” and “substituent” are also used interchangeably in this document. For purposes of this disclosure, “hydrocarbyl radical” is defined to be C1-C100 radicals, that may be linear, branched, or cyclic, and when cyclic, aromatic or non-aromatic. Examples of such radicals include, but are not limited to, methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, sec-butyl, tert-butyl, pentyl, iso-amyl, hexyl, octyl cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cyclooctyl, and the like including their substituted analogues. Substituted hydrocarbyl radicals are radicals in which at least one hydrogen atom of the hydrocarbyl radical has preferably been substituted with at least one halogen (such as Br, Cl, F or I) or at least one functional group such as NR*₂, OR*, SeR*, TeR*, PR*₂, AsR*₂, SbR*₂, SR*, BR*₂, SiR*₃, GeR*₃, SnR*₃, PbR*₃, and the like, or where at least one heteroatom has been inserted within a hydrocarbyl ring.

The term “alkenyl” or “hydrocarbenyl” means a straight-chain, branched-chain, or cyclic hydrocarbon radical having one or more double bonds that are not part of an aromatic ring. These alkenyl radicals may, optionally, be substituted. Examples of alkenyl radicals include, but are not limited to, ethenyl, propenyl, allyl, 1,4-butadienyl cyclopropenyl, cyclobutenyl, cyclopentenyl, cyclohexenyl, cyclooctenyl, and the like, including their substituted analogues.

The term “alkoxy” or “alkoxide” means an alkyl ether or aryl ether radical wherein the term alkyl is as defined above. Preferred “alkoxides” include those where the alkyl group is a C₁to C₁₀hydrocarbyl. The alkyl group may be straight chain, branched, or cyclic. The alkyl group may be saturated or unsaturated. In some embodiments, the alkyl group may comprise at least one aromatic group. Examples of suitable alkyl ether radicals include, but are not limited to, methoxy, ethoxy, n-propoxy, iso-propoxy, n-butoxy, iso-butoxy, sec-butoxy, tert-butoxy, phenoxyl, and the like.

The term “aryl” or “aryl group” means a six carbon aromatic ring and the substituted variants thereof, including but not limited to, phenyl, 2-methyl-phenyl, xylyl, 4-bromo-xylyl. Likewise, heteroaryl means an aryl group where a ring carbon atom (or two or three ring carbon atoms) has been replaced with a heteroatom, preferably N, O, or S. As used herein, the term “aromatic” also refers to pseudoaromatic heterocycles which are heterocyclic substituents that have similar properties and structures (nearly planar) to aromatic heterocyclic ligands, but are not by definition aromatic; likewise the term aromatic also refers to substituted aromatics.

Where isomers of a named alkyl, alkenyl, alkoxide, or aryl group exist (e.g., n-butyl, iso-butyl, sec-butyl, and tert-butyl) reference to one member of the group (e.g., n-butyl) shall expressly disclose the remaining isomers (e.g., iso-butyl, sec-butyl, and tert-butyl) in the family. Likewise, reference to an alkyl, alkenyl, alkoxide, or aryl group without specifying a particular isomer (e.g., butyl) expressly discloses all isomers (e.g., n-butyl, iso-butyl, sec-butyl, and tert-butyl).

The term “ring atom” means an atom that is part of a cyclic ring structure. By this definition, a benzyl group has six ring atoms and tetrahydrofuran has 5 ring atoms.

A heterocyclic ring is a ring having a heteroatom in the ring structure as opposed to a heteroatom substituted ring where a hydrogen on a ring atom is replaced with a heteroatom. For example, tetrahydrofuran is a heterocyclic ring and 4-N,N-dimethylamino-phenyl is a heteroatom substituted ring.

The term “continuous” means a system that operates without interruption or cessation. For example, a continuous process to produce a polymer would be one where the reactants are continually introduced into one or more reactors and polymer product is continually withdrawn.

A solution polymerization means a polymerization process in which the polymer is dissolved in a liquid polymerization medium, such as an inert solvent or monomer(s) or their blends. A solution polymerization is typically homogeneous. A homogeneous polymerization is one where the polymer product is dissolved in the polymerization medium. Such systems are preferably not turbid as described in J. Vladimir Oliveira, C. Dariva and J. C. Pinto, Ind. Eng. Chem. Res., 29, 2000, 4627.

A bulk polymerization means a polymerization process in which the monomers and/or comonomers being polymerized are used as a solvent or diluent using little or no inert solvent as a solvent or diluent. A small fraction of inert solvent might be used as a carrier for catalyst and scavenger. A bulk polymerization system contains less than 25 wt % of inert solvent or diluent, preferably less than 10 wt %, preferably less than 1 wt %, preferably 0 wt %.

Process

This invention relates to processes to produce branched ethylene-propylene-diene terpolymers comprising:

1) contacting monomers comprising propylene, ethylene and diene with a catalyst system comprising an activator (such as an alumoxane or non-coordinating anion activator), a metal hydrocarbenyl chain transfer agent (preferably an aluminum vinyl transfer agent), and one or more single site catalyst complexes, such as a quinolinyldiamido complex represented by the Formula I or II:

[Image Omitted]

wherein:

M is a Group 3, 4, 5, 6, 7, 8, 9, or 10 metal (preferably M is Zr or Hf);

E is C, Si or Ge;

X is an anionic leaving group (preferably X is methyl, chloride, or dialkylamido);

L is a neutral Lewis base (preferably L is ether, amine, phosphine, or thioether);

R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups (preferably R¹& R¹³are aryl groups, preferably R¹is 2,6-disubstituted aryl, preferably R¹is 2,6-diisopropylphenyl, preferably R¹³is 2-substituted aryl, preferably R¹³is phenyl, preferably R¹is 2,6-disubstituted aryl group and R¹³is an aryl group lacking substitution in the 2 and 6 positions);

R², R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are each independently selected from the group consisting of hydrogen, hydrocarbyls, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyls, halogen, and phosphino;

J is a divalent group that forms a three-atom-length bridge between the pyridine ring and the amido nitrogen (preferably J is selected from the following structures);

[Image Omitted]

n is 1 or 2;

m is 0, 1, or 2; and

two X groups may be joined together to form a dianionic group;

two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group;

adjacent groups from the following R², R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²may be joined to form a ring (preferably R⁷& R⁸are joined to form an aromatic ring, preferably R⁷& R⁸are joined with the joined R⁷R⁸group being CHCHCHCH, preferably R¹⁰& R¹¹are joined to form a five- or six-membered ring, preferably R¹⁰& R¹¹are joined, with the joined R¹⁰R¹¹group being CH₂CH₂or CH₂CH₂CH₂);

where the metal hydrocarbenyl chain transfer agent is represented by the formula:

Al(R′)_3-v(R″)_vor E[Al(R′)_2-y(R″)_y]₂, wherein each R′, independently, is a C₁to C₃₀hydrocarbyl group; each R″, independently, is a C₄to C₂₀hydrocarbenyl group having an allyl chain end; E is a group 16 element (such as O or S); v is from 0.01 to 3 (such as 1 or 2), and y is from 0.01 to 2, such as 1 or 2 (preferably the metal hydrocarbenyl chain transfer agent is an aluminum vinyl-transfer agent (AVTA) represented by the formula: Al(R′)_3-v(R)_vwith R defined as a hydrocarbenyl group containing 4 to 20 carbon atoms and featuring an allyl chain end, R′ defined as a hydrocarbyl group containing 1 to 30 carbon atoms, and v is 0.1 to 3 (such as 1 or 2)); and

2) obtaining branched ethylene-propylene-diene terpolymers comprising from about 98.9 to 30 wt % propylene, from 1 to 70 wt % ethylene, from 0.1 to 20 wt % diene monomer, and a remnant of the metal hydrocarbenyl chain transfer agent, wherein said branched ethylene-propylene-diene terpolymer: a) has a g′_visof less than 0.90; b) is essentially gel free (such as 5 wt % or less of xylene insoluble material); c) has an Mw of 250,000 g/mol or more; d) has a Mw/Mn of 3.0 or more; and e) has an Mz of 850,000 g/mol or more,

wherein the process preferably has a diene conversion of at least 15% (preferably at least 16%, preferably at least 16.5%) and the ratio of a metal hydrocarbenyl chain transfer agent (such as an aluminum vinyl transfer agent) to the one or more single site catalyst complexes is at least 100:1 (preferably at least 125:1 preferably at least 145:1, alternately from 100:1 to 1,000,000:1, alternately from 125:1 to 500,000:1, alternately from 145:100,000:1).

The catalyst/activator combinations are formed by combining the transition metal complex with activators in any manner known from the literature, including by supporting them for use in slurry or gas phase polymerization. The catalyst/activator combinations may also be added to or generated in solution polymerization or bulk polymerization (in the monomer). The metal hydrocarbenyl chain transfer agent (preferably an aluminum vinyl transfer agent) may be added to the catalyst and or activator before, during or after the activation of the catalyst complex or before or during polymerization. Typically, the metal hydrocarbenyl chain transfer agent (preferably the aluminum vinyl-transfer agent) is added to the polymerization reaction separately, such as before, the catalyst/activator pair.

The polymer produced from the polymerization using the catalyst systems described herein preferably contains at least 0.05 allyl chain ends per polymer chain, 0.1 allyl chain ends per polymer chain, at least 0.2 allyl chain ends per polymer chain, at least 0.3 allyl chain ends per polymer chain, at least 0.4 allyl chain ends per polymer chain, at least 0.5 allyl chain ends per polymer chain, at least 0.6 allyl chain ends per polymer chain, at least 0.7 allyl chain ends per polymer chain, at least 0.8 allyl chain ends per polymer chain, at least 0.8 allyl chain ends per polymer chain, at least 1.0 allyl chain ends per polymer chain. Ethylene-propylene-diene monomer copolymers are particularly preferred products. If the catalyst complex chosen is also capable of incorporating bulky alkene monomers, such as C₆to C₂₀alpha olefins, into the growing polymer chain, then the resulting polymer may contain long chain branches formed by the insertion of an allyl terminated polymer chain formed in situ (also referred to as a “vinyl-terminated macromonomer”) into the growing polymer chains. Process conditions including residence time, the ratio of monomer to polymer in the reactor, and the ratio of transfer agent to polymer will affect the amount of long chain branching in the polymer, the average length of branches, and the type of branching observed. A variety of branching types may be formed, which include comb architectures and branch on branch structures similar to those found in low-density polyethylene. The combination of chain growth and vinyl-group insertion may lead to polymer with a branched structure and having one or fewer vinyl unsaturations per polymer molecule. The absence of significant quantities of individual polymer molecules containing greater than one vinyl unsaturation prevents or reduces the formation of unwanted crosslinked polymers. Polymers having long chain branching typically have a g′_visof 0.97 or less, alternately 0.95 or less, alternately 0.90 or less, alternately 0.85 or less, alternately 0.80 or less, alternately 0.75 or less, alternately 0.70 or less, alternately 0.60 or less.

If the catalyst chosen is poor at incorporating comonomers such as C₂to C₂₀alpha olefins, then the polymer obtained is largely linear (little or no long chain branching). Likewise, process conditions including the ratio of transfer agent to polymer will affect the molecular weight of the polymer. Polymers having little or no long chain branching typically have a g′_visof more than 0.97, alternately 0.98 or more.

Alkene polymerizations and co-polymerizations using one or more transfer agents, such as an AVTA, with two or more catalysts are also of potential use. Desirable products that may be accessed with this approach includes polymers that have branch block structures and/or high levels of long-chain branching.

The transfer agent to catalyst complex equivalence ratio can be from about 100:1 to 500,000:1, preferably 115:1 to 450,000:1, preferably 125:1 to 400,000:1. Preferably, the molar ratio of transfer agent to catalyst complex is greater than one. Alternately, the molar ratio of transfer agent to catalyst complex is greater than 125:1. Preferably, the transfer agent is an aluminum vinyl transfer agent (AVTA) and the AVTA to catalyst complex equivalence ratio is greater than 100:1. Preferably the molar ratio of AVTA to catalyst complex is greater than 125:1. More preferred the molar ratio of AVTA to catalyst complex is greater than 145:1.

The AVTA can also be used in combination with other chain transfer agents that are typically used as scavengers, such as trialkylaluminum compounds (where the alkyl groups are selected from C₁to C₂₀alkyl groups, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, or an isomer thereof). Usefully the ATVA can be used in combination with a trialkyl aluminum compound such as tri-n-octylaluminum and triisobutylaluminum. The ATVA can also be used in combination with a dialkyl zinc compound, such as diethylzinc, dimethylzinc, or dipropylzinc.

The transfer agent can also be used in combination with oxygen-containing organoaluminums such as bis(diisobutylaluminum)oxide, MMAO-3A, and other alumoxanes. Certain of these oxygen-containing organoaluminums are expected to serve as scavengers while remaining significantly less prone to hydrocarbyl group chain-transfer than typical organoaluminums, such as trimethylaluminum or tri(n-octyl)aluminum.

The production of di-end-functionalized polymers is possible with this technology. One product, prior to exposure to air, from an alkene polymerization performed in the presence of AVTA is the aluminum-capped species Al(R′)_3-v(polymer-CH═CH₂)_v, where v is 0.1 to 3 (alternately 1 to 3, alternately 1, 2, or 3). The Al-carbon bonds will react with a variety of electrophiles (and other reagents), such as oxygen, halogens, carbon dioxide, and the like. Thus, quenching the reactive polymer mixture with an electrophile prior to exposure to atmosphere would yield a di-end-functionalized product of the general formula: Z-(monomers)_n-CH═CH₂, where Z is a group from the reaction with the electrophile and n is an integer, such as from 1 to 1,000,000, alternately from 2 to 50,000, alternately from 10 to 25,000, alternately from 3 to 900,000, alternately from 10,000 to 850,000, alternately from 20,000 to 800,000. For example, quenching with oxygen yields a polymer functionalized at one end with a hydroxy group and at the other end with a vinyl group. Quenching with bromine yields a polymer functionalized at one end with a Br group and at the other end with a vinyl group.

Functional group terminated polymers can also be produced using functional group transfer agents (FGTA). In this embodiment of the invention, the FGTA is represented by the formula M^FGTA(R′)_3-v(FG)_v, with R′ and v defined as above, M^FGTAa Group 13 element (such as B or Al), and with FG defined as a group containing 1 to 20 carbon atoms and a functional group Z. The choice of FG is such that it is compatible with the catalyst system being used. Preferred Z groups include, but are not limited to, non-vinyl olefinic groups such as vinylidene, vinylene or trisubstituted olefins, cyclics containing unsaturation such as cyclohexene, cyclooctene, vinyl cyclohexene, aromatics, ethers, and metal-capped alkoxides.

In another embodiment of the invention, the polymer products of this invention are of the formula: polymer-(CH₂)_nCH═CH₂where n is from 2 to 18, preferably from 6 to 14, more preferably 6, and where “polymer” is the attached polymeryl chain. Polymers of this formula are particularly well suited in making branch polymer combs. The polymer combs can be made by any number of methods. One method would be to use a catalyst system to make the vinyl terminated polymer, and then use a second catalyst system to incorporate the vinyl terminated polymer into a polymer backbone made from the second catalyst. This can be done sequentially in one reactor by first making the vinyl terminated polymer and then adding a second catalyst and, optionally, different monomer feeds in the same reactor. Alternatively, two reactors in series can be used where the first reactor is used to make the vinyl terminated polymer which flows into a second reactor in series having the second catalyst and, optionally, different monomer feeds. The vinyl terminated polymer can be a soft material, as in an ethylene propylene copolymer (such as ethylene propylene copolymer rubber), low density polyethylene, or a polypropylene, or a harder material, as in an isotactic polypropylene, high density polyethylene, or other polyethylene. Typically, if the vinyl terminated polymer is soft, it is useful if the polymer backbone of the comb is hard; if the vinyl terminated polymer is hard, it is useful the polymer backbone of the comb is soft, however any combination of polymer structures and types can be used.

In another embodiment of the invention, the vinyl-terminated polymers (VTPs) of this invention are of formula: polymer-(CH₂)_nCH═CH₂where n is from 2 to 18, preferably from 6 to 14, more preferably 6, and where “polymer” is the attached polymeryl chain. VTPs of this formula are particularly well suited in making branch block polymers. The branch block polymers can be made by any number of methods. One method involves using the same catalyst that is used to make the VTP, and then changing polymerization conditions (such as, but not limited to, by changing monomer composition and/or type and/or the amount or presence of AVTA) in the same or different reactor (such as two or more reactors in series). In this case, the branch will have a different polymeric composition vs. the polymer backbone created under the different polymerization conditions. Another method would be to use a catalyst system to make the VTP, then use a second catalyst system to incorporate the VTPs into a polymer backbone made from the second catalyst. This can be done sequentially in one reactor by first making the VTP and then adding a second catalyst and, optionally, different monomer feeds in the same reactor. Alternatively, two reactors in series can be used where the first reactor is used to make the VTP which flows into a second reactor in series having the second catalyst and, optionally, different monomer feeds. The branched block polymers can be of any composition, however, typically a combination of soft and hard polymers (relative to one another) are preferred. For example, an iPP VTP could be produced in a reactor, and then ethylene added to the existing propylene feed to make a rubber EP that would have iPP branches. Or an iPP VTP could be produced in a first reactor, and then sent to a second reactor containing ethylene (or additional ethylene for a propylene ethylene copolymer and, optionally, additional propylene monomer (and the same or different catalyst) to make a rubber EP that would have iPP branches (or propylene ethylene copolymer branches).

In any embodiment of this invention where the aluminum vinyl transfer agent is present, the aluminum vinyl transfer agent is present at a catalyst complex-to-aluminum vinyl transfer agent molar ratio of from about 1:3000 to 1:100, alternatively 1:2000 to 1:115, alternatively 1:1000 to 1:125.

In a preferred embodiment, the polymerization:

1) is conducted at temperatures of 80 to 300° C. (preferably 85 to 150° C., preferably 90 to 145° C., preferably 95 to 140° C.);

2) is conducted at a pressure of atmospheric pressure to 10 MPa (preferably 0.35 to 10 MPa, preferably from 0.45 to 6 MPa, preferably from 0.5 to 5 MPa);

3) is conducted in an aliphatic hydrocarbon solvent (such as isobutane, butane, pentane, isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons, such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof; preferably where aromatics are preferably present in the solvent at less than 1 wt %, preferably less than 0.5 wt %, preferably at 0 wt % based upon the weight of the solvents);

4) wherein the ratio of metal hydrocarbenyl transfer agent to catalyst is at least 100:1 (preferably 125:1 or more, preferably 145:1 or more);

5) the polymerization preferably occurs in one reaction zone;

6) the productivity of the catalyst compound is at least 80,000 g/mmol/hr (preferably at least 150,000 g/mmol/hr, preferably at least 200,000 g/mmol/hr, preferably at least 250,000 g/mmol/hr, preferably at least 300,000 g/mmol/hr);

7) the diene conversion is 15% or more, preferably 16% or more, preferably 16.5% or more; and

8) optionally hydrogen is present in the polymerization reactor at a partial pressure of 0.001 to 50 psig (0.007 to 345 kPa) (preferably from 0.01 to 25 psig (0.07 to 172 kPa), more preferably 0.1 to 10 psig (0.7 to 70 kPa)). In a preferred embodiment, the catalyst system used in the polymerization comprises no more than one catalyst compound. A “reaction zone” also referred to as a “polymerization zone” is a vessel where polymerization takes place, for example a batch reactor. When multiple reactors are used in either series or parallel configuration, each reactor is considered as a separate polymerization zone. For a multi-stage polymerization in both a batch reactor and a continuous reactor, each polymerization stage is considered as a separate polymerization zone. In a preferred embodiment, the polymerization occurs in one reaction zone.

Transition Metal Complex

Transition metal complexes useful herein are certain “non-metallocene” olefin polymerization catalysts that undergo alkyl group transfer with the AVTA at a rate that is much higher than the rate at which they undergo typical termination processes, such as beta hydride elimination or chain-transfer to monomer. The term “non-metallocene catalyst”, also known as “post-metallocene catalyst” describe transition metal complexes that do not feature any pi-coordinated cyclopentadienyl anion donors (or the like) and are useful the polymerization of olefins when combined with common activators.

Particularly useful single site catalyst complexes include quinolinyldiamido complexes represented by Formulae I and II:

[Image Omitted]

wherein:

M is a Group 3, 4, 5, 6, 7, 8, 9, or 10 metal (preferably M is Zr or Hf);

E is chosen from C, Si, and Ge;

X is an anionic leaving group (preferably X is methyl, chloride, or dialkylamido);

L is a neutral Lewis base (preferably L is ether, amine, phosphine, or thioether);

R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups (preferably R¹& R¹³are aryl groups, preferably R¹is 2,6-disubstituted aryl, preferably R¹is 2,6-diisopropylphenyl, preferably R¹³is 2-substituted aryl, preferably R¹³is phenyl, preferably R¹is 2,6-disubstituted aryl group and R¹³is an aryl group lacking substitution in the 2 and 6 positions);

R², R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are each independently selected from the group consisting of hydrogen, hydrocarbyls, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyls, halogen, and phosphino (preferably R¹¹& R¹²are hydrogen);

J is a divalent group that forms a three-atom-length bridge between the pyridine ring and the amido nitrogen (preferably J is selected from the following structures);

[Image Omitted]

n is 1 or 2;

m is 0, 1, or 2;

two X groups may be joined together to form a dianionic group;

two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

adjacent groups from the following R², R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²may be joined to form a ring (preferably R⁷& R⁸are joined to form an aromatic ring, preferably R⁷& R⁸are joined with the joined R⁷R⁸group being CHCHCHCH, preferably R¹⁰& R¹¹are joined to form a five- or six-membered ring, preferably R¹⁰& R¹¹are joined with the joined R¹⁰R¹¹group being CH₂CH₂or CH₂CH₂CH₂).

In a preferred embodiment, preferred R¹²-E-R¹¹groups include CH₂, CMe₂, SiMe₂, SiEt₂, SiPr₂, SiBu₂, SiPh₂, Si(aryl)₂, Si(alkyl)₂, CH(aryl), CH(Ph), CH(alkyl), and CH(2-isopropylphenyl), where alkyl is a C₁to C₄₀alkyl group (preferably C₁to C₂₀alkyl, preferably one or more of methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, and isomers thereof), aryl is a C₅to C₄₀aryl group (preferably a C₆to C₂₀aryl group, preferably phenyl or substituted phenyl, preferably phenyl, 2-isopropylphenyl, or 2-tertbutylphenyl).

In yet further embodiments, useful catalyst compounds include quinolinyldiamido metal complexes, such as those represented by the following Formula (6b):

[Image Omitted]

wherein

M is a group 4 metal, preferably hafnium; (2) N is nitrogen; R⁵⁴and R⁵⁵, being independently selected from the group consisting of hydrogen, hydrocarbyls, substituted hydrocarbyls, alkoxy, silyl, amino, aryloxy, halogen and phosphino, and R⁵⁴and R⁵⁵may be joined to form a saturated heterocyclic ring, or a saturated substituted heterocyclic ring where substitutions on the ring can join to form additional rings; R⁵¹and R⁵²are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, silylcarbyls and substituted silylcarbyl groups; each X* is independently a univalent anionic ligand, or two X*s are joined and bound to the metal atom to form a metallocycle ring, or two X*s are joined to form a chelating ligand, a diene ligand, or an alkylidene ligand; R⁶¹, R⁶², R⁶³, R⁶⁴, R⁶⁵, R⁶⁶are independently selected from the group consisting of hydrogen, hydrocarbyls, substituted hydrocarbyls, alkoxy, aryloxy, halogen, amino, and silyl, and wherein any one or more adjacent R⁶¹-R⁶⁶may be joined to form a substituted or unsubstituted hydrocarbyl or heterocyclic ring, wherein the ring has 5, 6, 7, or 8 ring atoms and where substitutions on the ring can join to form additional rings; each R⁷⁰-R⁷¹are independently selected from the group consisting of hydrogen, hydrocarbyls, substituted hydrocarbyls, alkoxy, aryloxy, halogen, amino, and silyl, and wherein any one or more adjacent R⁷⁰-R⁷¹may be joined to form a substituted or unsubstituted hydrocarbyl or heterocyclic ring, wherein the ring has 5, 6, 7, or 8 ring atoms and where substitutions on the ring can join to form additional rings, and t is 2 or 3 (corresponding to cyclopentyl and cyclohexyl rings, respectively).

In an embodiment of the invention, R⁶¹-R⁶⁶are hydrogen.

In an embodiment of the invention, each R⁷⁰and R⁷¹are independently hydrogen, and t is 2 or 3, preferably 2.

In an embodiment of the invention, each R⁵⁴and R⁵⁵are independently hydrogen, an alkyl group or an aryl group or substituted aryl group; preferably one or both R⁵⁴or R⁵⁵is hydrogen, or one R⁵⁴or R⁵⁵is hydrogen and the other is an aryl group or substituted aryl group. Preferred, but not limiting, aryl groups include phenyl and 2-methylphenyl, 2-ethylphenyl, 2-isopropylphenyl and naphthyl.

In an embodiment of the invention, R⁵²and R⁵¹are independently aryl or substituted aryl; preferably R⁵¹is a substituted phenyl group such as, but not limited to 2,6-diisopropylphenyl, 2,6-diethylphenyl, 2,6-dimethylphenyl, mesityl, and the like, and preferably R⁵²is phenyl or a substituted phenyl group such as, but not limited to 2-tolyl, 2-ethylphenyl, 2-propylphenyl, 2-trifluoromethylphenyl, 2-fluorophenyl, mesityl, 2,6-diisopropylphenyl, 2,6-diethylphenyl, 2,6-dimethylphenyl, 3,5-di-tert-butylphenyl, and the like.

In an embodiment of the invention, R⁵⁴, R⁵⁵, R⁶¹-R⁶⁶, each R⁷⁰-R⁷¹are hydrogen, R⁵²is phenyl, R⁵¹is 2,6-diisopropylphenyl and t is 2.

In an embodiment of the invention, R⁶²is joined with R⁶³to form a phenyl ring fused to the existing phenyl ring (e.g., a naphthyl group), and R⁶¹, R⁶⁴, R⁶⁵, and R⁶⁶are independently hydrogen or an alkyl group, preferably hydrogen.

In an embodiment of the invention, each R⁵⁴and R⁵⁵are independently hydrogen, an alkyl group or an aryl group or substituted aryl group; preferably one or both R⁵⁴or R⁵⁵is hydrogen, or one R⁵⁴or R⁵⁵is hydrogen and the other is an aryl group or substituted aryl group. Preferred, but not limiting, aryl groups for R⁵⁴or R⁵⁵include phenyl, 2-methylphenyl, 2-ethylphenyl, 2-isopropylphenyl, and naphthyl.

Non-limiting examples of quinolinyldiamido catalysts that are useful herein are illustrated below, wherein X is methyl, benzyl, or chloro:

[Image Omitted]

A particularly preferred catalyst is

[Image Omitted]

Additional quinolinyldiamido transition metal complexes useful herein are described in US2018-0002352 and are incorporated by reference.

The quinolinyldiamido ligands described herein are generally prepared in multiple steps in accordance with the disclosure of US2018-0002352. An important step involves the preparation of a suitable “linker” group(s) containing both an aryl boronic acid (or acid ester) and an amine group. Examples of these include compounds of the general formula: 7-(boronic acid)-2,3-dihydro-1H-inden-1-(amine), 7-(boronic acid ester)-2,3-dihydro-1H-1-(amine), 7-(boronic acid)-1,2,3,4-tetrahydronaphthalen-1-(amine), 7-(boronic acid ester)-1,2,34-tetrahydronaphthalen-1-(amine), which include various boronic acids, boronic acid esters, and amines. The linker groups may be prepared in high yield from arylhalide precursors containing amine functionality by first deprotonation of the amine group with 1.0 molar equivalents of n-BuLi, followed by transmetallation of an arylhalide with t-BuLi and subsequent reaction with a boron-containing reagent. This amine-containing linker is then coupled with a suitable quinoline containing species, such as 6-bromo-2-quinolinecarboxaldehyde. This coupling step typically uses a metal catalyst (e.g., Pd(PPh₃)₄) in less than 5 mol % loading. Following this coupling step, the new derivative, which can be described as amine-linker-quinoline-aldehyde, is then reacted with a second amine to produce the imine derivative amine-linker-quinoline-imine in a condensation reaction. This can then be reduced to the quinoline diamine ligand by reaction with a suitable aryl anion, alkyl anion, or hydride source. This reaction is generally performed in etherial solvents at temperatures between −100° C. and 50° C. when aryllithium or alkyllithium reagents are employed. This reaction is generally performed in methanol at reflux when sodium cyanoborohydride is employed.

The preparation of quinolinyldiamido metal complexes from quinoline diamines may be accomplished using typical protonolysis and methylation reactions. In the protonolysis reaction the quinoline diamine is reacted with a suitable metal reactant to produce a quinolinyldiamido metal complex. A suitable metal reactant will feature a basic leaving group that will accept a proton from the quinoline diamine and then generally depart and be removed from the product. Suitable metal reactants include, but are not limited to, HfBn₄(Bn═CH₂Ph), ZrBn₄, TiBn₄, ZrBn₂Cl₂(OEt₂), HfBn₂Cl₂(OEt₂)₂, Zr(NMe₂)₂Cl₂(dimethoxyethane), Hf(NMe₂)₂Cl₂(dimethoxyethane), Hf(NMe₂)₄, and Hf(NEt₂)₄. Quinolinyldiamido metal complexes that contain metal-chloride groups can be alkylated by reaction with an appropriate organometallic reagent. Suitable reagents include organolithium and organomagnesium, and Grignard reagents. The alkylations are generally performed in etherial or hydrocarbon solvents or solvent mixtures at temperatures typically ranging from −100° C. to 50° C.

In a preferred embodiment of the invention, the transition metal complex is not a metallocene. A metallocene catalyst is defined as an organometallic compound with at least one π-bound cyclopentadienyl moiety (or substituted cyclopentadienyl moiety) and more frequently two π-bound cyclopentadienyl moieties or substituted cyclopentadienyl moieties.

Usefully, the single site catalyst compounds useful herein are preferably tridentateligands bound to the transition metal (such as a group 4 metal), preferably tridentate N,N,N ligands bound to a transition metal (such as a Zr, Hf, or Ti).

In a preferred embodiment, the catalyst complexes are represented by the Formula (Ia) or (IIa):

[Image Omitted]

wherein:

M is a Group 4 metal;

J is a three-atom-length bridge between the quinoline and the amido nitrogen;

E* is carbon;

X is an anionic leaving group;

L is a neutral Lewis base;

R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups;

R²* and R³through R¹²are independently selected from the group consisting of hydrogen, hydrocarbyls, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyls, halogen, and phosphino;

n is 1 or 2;

m is 0, 1, or 2

n+m is not greater than 4;

any two adjacent R groups (e.g., R¹& R², R²& R³, etc.) may be joined to form a substituted or unsubstituted hydrocarbyl or heterocyclic ring, where the ring has 5, 6, 7, or 8 ring atoms and where substitutions on the ring can join to form additional rings;

any two X groups may be joined together to form a dianionic group;

any two L groups may be joined together to form a bidentate Lewis base; and

an X group may be joined to an L group to form a monoanionic bidentate group.

Preferably, in formula Ia and IIa, M is Hf, Zr or Ti;

J is group comprising a three-atom-length bridge between the quinoline and the amido nitrogen, preferably a group containing up to 50 non-hydrogen atoms;

E* is carbon;

X is a hydrocarbyl group or a halogen;

L is a neutral Lewis base;

R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups;

R²*, R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are independently hydrogen, hydrocarbyl, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyl, halogen, or phosphino;

n is 1 or 2;

m is 0, 1, or 2, where

n+m is not greater than 4;

any two adjacent R groups (e.g., R¹& R², R²& R³, etc.) may be joined to form a substituted hydrocarbyl, unsubstituted hydrocarbyl, substituted heterocyclic ring, or unsubstituted heterocyclic ring, where the ring has 5, 6, 7, or 8 ring atoms and where substitutions on the ring can join to form additional rings;

any two X groups may be joined together to form a dianionic group;

any two L groups may be joined together to form a bidentate Lewis base; and

any X group may be joined to an L group to form a monoanionic bidentate group.

Preferably, M is zirconium or hafnium.

In a preferred embodiment, J is an aromatic substituted or unsubstituted hydrocarbyl (preferably a hydrocarbyl) having from 3 to 30 non-hydrogen atoms, preferably J is represented by the Formula:

[Image Omitted]

where R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are as defined above, E is carbon, and any two adjacent R groups (e.g., R⁷& R⁸, R⁸& R⁹, R⁹& R¹⁰, R¹⁰& R¹¹, etc.) may be joined to form a substituted or unsubstituted hydrocarbyl or heterocyclic ring, where the ring has 5, 6, 7, or 8 ring atoms (preferably 5 or 6 atoms), and said ring may be saturated or unsaturated (such as partially unsaturated or aromatic), preferably J is an arylalkyl (such as arylmethyl, etc.) or dihydro-1H-indenyl, or tetrahydronaphthalenyl group.

In embodiments of the invention, J is selected from the following structures:

[Image Omitted]

where [Image Omitted] indicates connection to the complex.

In embodiments of the invention, X is alkyl (such as alkyl groups having 1 to 10 carbons, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, and isomers thereof), aryl, hydride, alkylsilane, fluoride, chloride, bromide, iodide, triflate, carboxylate, amido (such as NMe₂), or alkylsulfonate.

In embodiments of the invention, L is an ether, amine or thioether.

In embodiments of the invention, R⁷and R⁸are joined to form a six-membered aromatic ring with the joined R⁷R⁸group being —CH═CHCH═CH—.

In embodiments of the invention, R¹⁰and R¹¹are joined to form a five-membered ring with the joined R¹⁰R¹¹group being —CH₂CH₂—.

In embodiments of the invention, R¹⁰and R¹¹are joined to form a six-membered ring with the joined R¹⁰R¹¹group being —CH₂CH₂CH₂—.

In embodiments of the invention, R¹and R¹³may be independently selected from phenyl groups that are variously substituted with between zero to five substituents that include F, Cl, Br, I, CF₃, NO₂, alkoxy, dialkylamino, aryl, and alkyl groups having 1 to 10 carbons, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, and isomers thereof.

In a preferred embodiment of the invention, the quinolinyldiamido transition metal complex is represented by the Formula IIa above where: M is a Group 4 metal (preferably hafnium); E* is selected carbon; X is an alkyl, aryl, hydride, alkylsilane, fluoride, chloride, bromide, iodide, triflate, carboxylate, amido, alkoxo, or alkylsulfonate; L is an ether, amine, or thioether; R¹and R¹³are independently selected from the group consisting of hydrocarbyls, substituted hydrocarbyls, and silyl groups (preferably aryl); R²*, R³, R⁴, R⁵, R⁶, R⁷, R⁸, R⁹, R¹⁰, R¹¹, and R¹²are independently hydrogen, hydrocarbyl, alkoxy, silyl, amino, aryloxy, substituted hydrocarbyls, halogen, and phosphino; n is 1 or 2; m is 0, 1, or 2; n+m is from 1 to 4; and two X groups may be joined together to form a dianionic group; two L groups may be joined together to form a bidentate Lewis base; an X group may be joined to an L group to form a monoanionic bidentate group; R⁷and R⁸may be joined to form a ring (preferably an aromatic ring, a six-membered aromatic ring with the joined R⁷R⁸group being —CH═CHCH═CH—); R¹⁰and R¹¹may be joined to form a ring (preferably a five-membered ring with the joined R¹⁰R¹¹group being —CH₂CH₂—, a six-membered ring with the joined R¹⁰R¹¹group being —CH₂CH₂CH₂—).

In embodiments of Formula Ia and IIa, R⁴, R⁵, and R⁶are independently selected from the group consisting of hydrogen, hydrocarbyls, substituted hydrocarbyls, alkoxy, aryloxy, halogen, amino, and silyl, and wherein adjacent R groups (R⁴& R⁵and/or R⁵& R⁶) may be joined to form a substituted hydrocarbyl, unsubstituted hydrocarbyl, unsubstituted heterocyclic ring or substituted heterocyclic ring, where the ring has 5, 6, 7, or 8 ring atoms and where substitutions on the ring can join to form additional rings.

In embodiments of Formula Ia and IIa, R⁷, R⁸, R⁹, and R¹⁰are independently selected from the group consisting of hydrogen, hydrocarbyls, substituted hydrocarbyls, alkoxy, halogen, amino, and silyl, and wherein adjacent R groups (R⁷and R⁸, and/or R⁹and R¹⁰) may be joined to form a saturated, substituted hydrocarbyl, unsubstituted hydrocarbyl, unsubstituted heterocyclic ring or substituted heterocyclic ring, where the ring has 5, 6, 7, or 8 ring carbon atoms and where substitutions on the ring can join to form additional rings.

In embodiments of Formula Ia or IIa, R²* and R³are each, independently, selected from the group consisting of hydrogen, hydrocarbyls, and substituted hydrocarbyls, alkoxy, silyl, amino, aryloxy, halogen, and phosphino, R²* and R³may be joined to form a saturated, substituted or unsubstituted hydrocarbyl ring, where the ring has 4, 5, 6, or 7 ring carbon atoms and where substitutions on the ring can join to form additional rings, or R²* and R³may be joined to form a saturated heterocyclic ring, or a saturated substituted heterocyclic ring where substitutions on the ring can join to form additional rings.

In embodiments of Formula Ia or IIa, R¹¹and R¹²are each, independently, selected from the group consisting of hydrogen, hydrocarbyls, and substituted hydrocarbyls, alkoxy, silyl, amino, aryloxy, halogen, and phosphino, R¹¹and R¹²may be joined to form a saturated, substituted or unsubstituted hydrocarbyl ring, where the ring has 4, 5, 6, or 7 ring carbon atoms and where substitutions on the ring can join to form additional rings, or R¹¹and R¹²may be joined to form a saturated heterocyclic ring, or a saturated substituted heterocyclic ring where substitutions on the ring can join to form additional rings.

In embodiments of Formula Ia or IIa, R¹and R¹³may be independently selected from phenyl groups that are variously substituted with between zero to five substituents that include F, Cl, Br, I, CF₃, NO₂, alkoxy, dialkylamino, aryl, and alkyl groups having 1 to 10 carbons, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, and isomers thereof.

In embodiments of Formula IIa, preferred R¹²-E*-R¹¹groups include CH₂, CMe₂, Si(aryl)₂, Si(alkyl)₂, CH(aryl), CH(Ph), CH(alkyl), and CH(2-isopropylphenyl), where alkyl is a C₁to C₄₀alkyl group (preferably C₁to C₂₀alkyl, preferably one or more of methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, and isomers thereof), aryl is a C₅to C₄₀aryl group (preferably a C₆to C₂₀aryl group, preferably phenyl or substituted phenyl, preferably phenyl, 2-isopropylphenyl, or 2-tertbutylphenyl).

Preferably, the R groups above and other R groups mentioned hereafter, contain from 1 to 30, preferably from 2 to 20 carbon atoms, especially from 6 to 20 carbon atoms.

Preferably, M is Ti, Zr, or Hf, and E is carbon, with Zr or Hf based complexes being especially preferred.

In any embodiment of Formula IIa, described herein, E* is carbon and R¹²and R¹¹are independently selected from phenyl groups that are substituted with 0, 1, 2, 3, 4, or 5 substituents selected from the group consisting of F, Cl, Br, I, CF₃, NO₂, alkoxy, dialkylamino, hydrocarbyl, and substituted hydrocarbyl groups with from one to ten carbons.

In any embodiment described herein of Formula IIa, R¹¹and R¹²are independently selected from hydrogen, methyl, ethyl, phenyl, isopropyl, isobutyl, and trimethylsilyl.

In any embodiment described herein of Formula IIa, R⁷, R⁸, R⁹, and R¹⁰are independently selected from hydrogen, methyl, ethyl, propyl, isopropyl, phenyl, cyclohexyl, fluoro, chloro, methoxy, ethoxy, phenoxy, and trimethylsilyl.

In any embodiment described herein of Formula Ia or IIa, R²*, R³, R⁴, R⁵, and R⁶are independently selected from the group consisting of hydrogen, hydrocarbyls, alkoxy, silyl, amino, substituted hydrocarbyls, and halogen.

In any embodiment described herein of Formula Ia or IIa, each L is independently selected from Et₂O, MeOtBu, Et₃N, PhNMe₂, MePh₂N, tetrahydrofuran, and dimethylsulfide.

In any embodiment described herein of Formula I or II, each X is independently selected from methyl, benzyl, trimethylsilyl, neopentyl, ethyl, propyl, butyl, phenyl, hydrido, chloro, fluoro, bromo, iodo, dimethylamido, diethylamido, dipropylamido, and diisopropylamido.

In any embodiment described herein of Formula Ia or IIa, R¹is 2,6-diisopropylphenyl, 2,4,6-triisopropylphenyl, 2,6-diisopropyl-4-methylphenyl, 2,6-diethylphenyl, 2-ethyl-6-isopropylphenyl, 2,6-bis(3-pentyl)phenyl, 2,6-dicyclopentylphenyl, or 2,6-dicyclohexylphenyl.

In any embodiment described herein of Formula Ia, IIa, I or II, R¹³is phenyl, 2-methylphenyl, 2-ethylphenyl, 2-propylphenyl, 2,6-dimethylphenyl, 2-isopropylphenyl, 4-methylphenyl, 3,5-dimethylphenyl, 3,5-di-tert-butylphenyl, 4-fluorophenyl, 3-methylphenyl, 4-dimethylaminophenyl, or 2-phenylphenyl.

In any embodiment described herein of Formula IIa, J is dihydro-1H-indenyl and R¹is 2,6-dialkylphenyl or 2,4,6-trialkylphenyl.

In any embodiment described herein of Formula Ia or IIa, R¹is 2,6-diisopropylphenyl and R¹³is a hydrocarbyl group containing 1, 2, 3, 4, 5, 6, or 7 carbon atoms.

For information on how to synthesize such complexes please see U.S. Ser. No. 62/357,033, filed Jun. 30, 2016 (published as US 2018-0002352).

Activators

The catalyst systems typically comprise a transition metal complex as described above and an activator such as alumoxane or a non-coordinating anion. Activation may be performed using alumoxane solution including methyl alumoxane, referred to as MAO, as well as modified MAO, referred to herein as MMAO, containing some higher alkyl groups to improve the solubility. Particularly useful MAO can be purchased from Albemarle or Grace, typically in a 10 wt % solution in toluene. The catalyst system employed in the present invention may use an activator selected from alumoxanes, such as methyl alumoxane, modified methyl alumoxane, ethyl alumoxane, iso-butyl alumoxane, and the like.

When an alumoxane or modified alumoxane is used, the complex-to-activator molar ratio is from about 1:3000 to 10:1; alternatively 1:2000 to 10:1; alternatively 1:1000 to 10:1; alternatively, 1:500 to 1:1; alternatively 1:300 to 1:1; alternatively 1:200 to 1:1; alternatively 1:100 to 1:1; alternatively 1:50 to 1:1; alternatively 1:10 to 1:1. When the activator is an alumoxane (modified or unmodified), some embodiments select the maximum amount of activator at a 5000-fold molar excess over the catalyst precursor (per metal catalytic site). The preferred minimum activator-to-complex ratio is 1:1 molar ratio.

Activation may also be performed using non-coordinating anions, referred to as NCA's, of the type described in EP 277 003 A1 and EP 277 004 A1. NCA may be added in the form of an ion pair using, for example, [DMAH]+ [NCA]− in which the N,N-dimethylanilinium (DMAH) cation reacts with a basic leaving group on the transition metal complex to form a transition metal complex cation and [NCA]−. The cation in the precursor may, alternatively, be trityl. Alternatively, the transition metal complex may be reacted with a neutral NCA precursor, such as B(C₆F5)₃, which abstracts an anionic group from the complex to form an activated species. Useful activators include N,N-dimethylanilinium tetrakis (pentafluorophenyl)borate (i.e., [PhNMe₂H]B(C₆F₅)₄) and N,N-dimethylanilinium tetrakis (heptafluoronaphthyl)borate, where Ph is phenyl, and Me is methyl.

Additionally, preferred activators useful herein include those described in U.S. Pat. No. 7,247,687 at column 169, line 50 to column 174, line 43, particularly column 172, line 24 to column 173, line 53.

In an embodiment of the invention described herein, the non-coordinating anion activator is represented by the following Formula (1):

(Z)_d⁺(A^d−) (1)

wherein Z is (L-H) or a reducible Lewis acid; L is a neutral Lewis base; H is hydrogen and (L-H)⁺ is a Bronsted acid; A^d− is a non-coordinating anion having the charge d−; and d is an integer from 1 to 3.

When Z is (L-H) such that the cation component is (L-H)d⁺, the cation component may include Bronsted acids such as protonated Lewis bases capable of protonating a moiety, such as an alkyl or aryl, from the catalyst precursor, resulting in a cationic transition metal species, or the activating cation (L-H)d⁺ is a Bronsted acid, capable of donating a proton to the catalyst precursor resulting in a transition metal cation, including ammoniums, oxoniums, phosphoniums, silyliums, and mixtures thereof, or ammoniums of methylamine, aniline, dimethylamine, diethylamine, N-methylaniline, diphenylamine, trimethylamine, triethylamine, N,N-dimethylaniline, methyldiphenylamine, pyridine, p-bromo N,N-dimethylaniline, p-nitro-N,N-dimethylaniline, phosphoniums from triethylphosphine, triphenylphosphine, and diphenylphosphine, oxoniums from ethers, such as dimethyl ether diethyl ether, tetrahydrofuran, and dioxane, sulfoniums from thioethers, such as diethyl thioethers and tetrahydrothiophene, and mixtures thereof.

When Z is a reducible Lewis acid, it may be represented by the formula: (Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, or a C₁to C₄₀hydrocarbyl, the reducible Lewis acid may be represented by the formula: (Ph₃C⁺), where Ph is phenyl or phenyl substituted with a heteroatom, and/or a C₁to C₄₀hydrocarbyl. In an embodiment, the reducible Lewis acid is triphenyl carbenium.

Embodiments of the anion component Ad⁻ include those having the formula [Mk+Qn]d⁻ wherein k is 1, 2, or 3; n is 1, 2, 3, 4, 5, or 6, or 3, 4, 5, or 6; n−k=d; M is an element selected from Group 13 of the Periodic Table of the Elements, or boron or aluminum, and Q is independently a hydride, bridged or unbridged dialkylamido, halide, alkoxide, aryloxide, hydrocarbyl radicals, said Q having up to 20 carbon atoms with the proviso that in not more than one occurrence is Q a halide, and two Q groups may form a ring structure. Each Q may be a fluorinated hydrocarbyl radical having 1 to 20 carbon atoms, or each Q is a fluorinated aryl radical, or each Q is a pentafluoryl aryl radical. Examples of suitable Ad− components also include diboron compounds as disclosed in U.S. Pat. No. 5,447,895, which is fully incorporated herein by reference.

In an embodiment in any of the NCA's represented by Formula 1 described above, the anion component Ad− is represented by the formula [M*k*+Q*n*]d*− wherein k* is 1, 2, or 3; n* is 1, 2, 3, 4, 5, or 6 (or 1, 2, 3, or 4); n*−k*=d*; M* is boron; and Q* is independently selected from hydride, bridged or unbridged dialkylamido, halogen, alkoxide, aryloxide, hydrocarbyl radicals, said Q* having up to 20 carbon atoms with the proviso that in not more than 1 occurrence is Q* a halogen.

This invention also relates to a method to polymerize olefins comprising contacting olefins (such as ethylene, propylene and diene monomers) with a catalyst complex as described above and an NCA activator represented by the Formula (2):

R_nM**(ArNHal)_4-n (2)

where R is a monoanionic ligand; M** is a Group 13 metal or metalloid; ArNHal is a halogenated, nitrogen-containing aromatic ring, polycyclic aromatic ring, or aromatic ring assembly in which two or more rings (or fused ring systems) are joined directly to one another or together; and n is 0, 1, 2, or 3. Typically the NCA comprising an anion of Formula 2 also comprises a suitable cation that is essentially non-interfering with the ionic catalyst complexes formed with the transition metal compounds, or the cation is Z_d⁺ as described above.

In an embodiment in any of the NCA's comprising an anion represented by Formula 2 described above, R is selected from the group consisting of C₁to C₃₀hydrocarbyl radicals. In an embodiment, C₁to C₃₀hydrocarbyl radicals may be substituted with one or more C₁to C₂₀hydrocarbyl radicals, halide, hydrocarbyl substituted organometalloid, dialkylamido, alkoxy, aryloxy, alkysulfido, arylsulfido, alkylphosphido, arylphosphide, or other anionic substituent; fluoride; bulky alkoxides, where bulky means C₄to C₂₀hydrocarbyl radicals; —SRa, —NRa₂, and —PRa₂, where each Ra is independently a monovalent C₄to C₂₀hydrocarbyl radical comprising a molecular volume greater than or equal to the molecular volume of an isopropyl substitution or a C₄to C₂₀hydrocarbyl substituted organometalloid having a molecular volume greater than or equal to the molecular volume of an isopropyl substitution.

In an embodiment in any of the NCA's comprising an anion represented by Formula 2 described above, the NCA also comprises cation comprising a reducible Lewis acid represented by the formula: (Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, and/or a C₁to C₄₀hydrocarbyl, or the reducible Lewis acid represented by the formula: (Ph₃C⁺), where Ph is phenyl or phenyl substituted with one or more heteroatoms, and/or C₁to C₄₀hydrocarbyls.

In an embodiment in any of the NCA's comprising an anion represented by Formula 2 described above, the NCA may also comprise a cation represented by the formula, (L-H)d⁺, wherein L is a neutral Lewis base; H is hydrogen; (L-H) is a Bronsted acid; and d is 1, 2, or 3, or (L-H)d⁺ is a Bronsted acid selected from ammoniums, oxoniums, phosphoniums, silyliums, and mixtures thereof.

Further examples of useful activators include those disclosed in U.S. Pat. No. 7,297,653 and U.S. Pat. No. 7,799,879, which are fully incorporated by reference herein.

In an embodiment, an activator useful herein comprises a salt of a cationic oxidizing agent and a noncoordinating, compatible anion represented by the Formula (3):

(OX^e+)_d(A^d−)_e (3)

wherein OX^e+ is a cationic oxidizing agent having a charge of e+; e is 1, 2, or 3; d is 1, 2, or 3; and A^d− is a non-coordinating anion having the charge of d− (as further described above). Examples of cationic oxidizing agents include: ferrocenium, hydrocarbyl-substituted ferrocenium, Ag⁺, or Pb⁺². Suitable embodiments of A^d− include tetrakis(pentafluorophenyl)borate.

Activators useful in catalyst systems herein include: trimethylammonium tetrakis(perfluoronaphthyl)borate, N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate, N,N-diethylanilinium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, trimethylammonium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, and the types disclosed in U.S. Pat. No. 7,297,653, which is fully incorporated by reference herein.

Suitable activators also include: N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(perfluorophenyl)borate, [Ph₃C+][B(C₆F₅)₄—], [Me₃NH+][B(C₆F₅)₄—]; 1-(4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluorophenyl)pyrrolidinium; and tetrakis(pentafluorophenyl)borate, 4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluoropyridine.

In an embodiment, the activator comprises a triaryl carbonium (such as triphenylcarbenium tetraphenylborate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate).

In an embodiment, two NCA activators may be used in the polymerization and the molar ratio of the first NCA activator to the second NCA activator can be any ratio. In an embodiment, the molar ratio of the first NCA activator to the second NCA activator is 0.01:1 to 10,000:1, or 0.1:1 to 1000:1, or 1:1 to 100:1.

In an embodiment of the invention, the NCA activator-to-catalyst ratio is a 1:1 molar ratio, or 0.1:1 to 100:1, or 0.5:1 to 200:1, or 1:1 to 500:1 or 1:1 to 1000:1. In an embodiment, the NCA activator-to-catalyst ratio is 0.5:1 to 10:1, or 1:1 to 5:1.

In an embodiment, the catalyst compounds can be combined with combinations of alumoxanes and NCA's (see for example, U.S. Pat. No. 5,153,157; U.S. Pat. No. 5,453,410; EP 0 573 120 BI; WO 94/07928; and WO 95/14044 which discuss the use of an alumoxane in combination with an ionizing activator, all of which are incorporated by reference herein).

In a preferred embodiment of the invention, when an NCA (such as an ionic or neutral stoichiometric activator) is used, the complex-to-activator molar ratio is typically from 1:10 to 1:1; 1:10 to 10:1; 1:10 to 2:1; 1:10 to 3:1; 1:10 to 5:1; 1:2 to 1.2:1; 1:2 to 10:1; 1:2 to 2:1; 1:2 to 3:1; 1:2 to 5:1; 1:3 to 1.2:1; 1:3 to 10:1; 1:3 to 2:1; 1:3 to 3:1; 1:3 to 5:1; 1:5 to 1:1; 1:5 to 10:1; 1:5 to 2:1; 1:5 to 3:1; 1:5 to 5:1; 1:1 to 1:1.2.

Alternately, a co-activator or chain transfer agent, such as a group 1, 2, or 13 organometallic species (e.g., an alkyl aluminum compound such as tri-n-octyl aluminum), may also be used in the catalyst system herein. The complex-to-co-activator molar ratio is from 1:100 to 100:1; 1:75 to 75:1; 1:50 to 50:1; 1:25 to 25:1; 1:15 to 15:1; 1:10 to 10:1; 1:5 to 5:1; 1:2 to 2:1; 1:100 to 1:1; 1:75 to 1:1; 1:50 to 1:1; 1:25 to 1:1; 1:15 to 1:1; 1:10 to 1:1; 1:5 to 1:1; 1:2 to 1:1; 1:10 to 2:1.

Metal Hydrocarbenyl Transfer Agents (Aluminum Vinyl Transfer Agents)

The catalyst systems described herein further comprise a metal hydrocarbenyl transfer agent (which is any group 13 metal agent that contains at least one transferrable group that has an allyl chain end), preferably an aluminum vinyl-transfer agent, also referred to as an AVTA, (which is any aluminum agent that contains at least one transferrable group that has an allyl chain end). An allyl chain end is represented by the formula H₂C═CH—CH₂—. “Allylic vinyl group,” “allyl chain end,” “vinyl chain end,” “vinyl termination,” “allylic vinyl group,” “terminal vinyl group,” and “vinyl terminated” are used interchangeably herein and refer to an allyl chain end. An allyl chain end is not a vinylidene chain end or a vinylene chain end. The number of allyl chain ends, vinylidene chain ends, vinylene chain ends, and other unsaturated chain ends is determined using ¹H NMR at 120° C. using deuterated tetrachloroethane as the solvent on an at least 250 MHz NMR spectrometer.

Useful transferable groups containing an allyl chain end are represented by the formula CH₂═CH—CH₂—R*, where R* represents a hydrocarbyl group or a substituted hydrocarbyl group, such as a C₁to C₂₀alkyl, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, or an isomer thereof.

In the catalyst system described herein, the catalyst undergoes alkyl group transfer with the transfer agent, which enables the formation of polymer chains containing one or more allyl chain ends.

Useful transferable groups containing an allyl chain end also include those represented by the formula CH₂═CH—CH₂—R**, where R** represents a hydrocarbeneyl group or a substituted hydrocarbeneyl group, such as a C₁to C₂₀alkylene, preferably methylene (CH₂), ethylene [(CH₂)₂], propandiyl [(CH₂)₂], butandiyl [(CH₂)₄], pentandiyl [(CH₂)₅], hexandiyl [(CH₂)₆], heptandiyl [(CH₂)₇], octandiyl [(CH₂)₈], nonandiyl [(CH₂)₉], decandiyl [(CH₂)₁₀], undecandiyl [(CH₂₀)₁₁], dodecandiyl [(CH₂)₁₂], or an isomer thereof. Useful transferable groups are preferably non-substituted linear hydrocarbeneyl groups. Preferably, at least one R** is a C₄-C₂₀hydrocarbenyl group.

The term “hydrocarbenyl” refers to a hydrocarb-di-yl divalent group, such as a C₁to C₂₀alkylene (i.e., methylene (CH₂), ethylene [(CH₂)₂], propandiyl [(CH₂)₃], butandiyl [(CH₂)₄], pentandiyl [(CH₂)₅], hexandiyl [(CH₂)₆], heptandiyl [(CH₂)₇], octandiyl [(CH₂)₈], nonandiyl [(CH₂)₉], decandiyl [(CH₂)₁₀], undecandiyl [(CH₂)₁₁], dodecandiyl [(CH₂)₁₂], and isomers thereof).

AVTA's are alkenylaluminum reagents capable of causing group exchange between the transition metal of the catalyst system (M^TM) and the metal of the AVTA (M^AVTA). The reverse reaction may also occur such that the polymeryl chain is transferred back to the transition metal of the catalyst system. This reaction scheme is illustrated below:

[Image Omitted]

wherein M^TMis an active transition metal catalyst site and P is the polymeryl chain, M^AVTAis the metal of the AVTA, and R is a transferable group containing an allyl chain end, such as a hydrocarbyl group containing an allyl chain end, also called a hydrocarbenyl or alkenyl group.

Catalyst systems of this invention preferably have high rates of olefin propagation and negligible or no chain termination via beta hydride elimination, beta methyl elimination, or chain transfer to monomer relative to the rate of chain transfer to the AVTA or other chain transfer agent, such as an aluminum alkyl, if present. Pyridyldiamido catalyst complexes (see U.S. Pat. No. 7,973,116; U.S. Pat. No. 8,394,902; U.S. Pat. No. 8,674,040; U.S. Pat. No. 8,710,163; U.S. Pat. No. 9,102,773; US 2014/0256893; US 2014/0316089; and US 2015/0141601) activated with non-coordinating activators such as dimethylanilinium tetrakis(perfluorophenyl)borate and/or dimethylanilinium tetrakis(perfluoronaphthyl)borate are particularly useful in the catalyst systems of this invention. Compound 3, described above is particularly preferred.

In any embodiment of the invention described herein, the catalyst system comprises an aluminum vinyl transfer agent, which is typically represented by the formula (I):

Al(R′)_3-v(R)_v

where R is a hydrocarbenyl group containing 4 to 20 carbon atoms having an allyl chain end, R′ is a hydrocarbyl group containing 1 to 30 carbon atoms, and v is 0.1 to 3, alternately 1 to 3, alternately 1.1 to less than 3, alternately v is 0.5 to 2.9, 1.1 to 2.9, alternately 1.5 to 2.7, alternately 1.5 to 2.5, alternately 1.8 to 2.2. The compounds represented by the formula Al(R′)_3-v(R)_vare typically a neutral species, but anionic formulations may be envisioned, such as those represented by formula (II): [Al(R′)_4-w(R)_w]⁻, where w is 0.1 to 4, R is a hydrocarbenyl group containing 4 to 20 carbon atoms having an allyl chain end, and R′ is a hydrocarbyl group containing 1 to 30 carbon atoms.

In any embodiment of any formula for a metal hydrocarbenyl chain transfer agent described herein, each R′ is independently chosen from C₁to C₃₀hydrocarbyl groups (such as a C₁to C₂₀alkyl groups, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, or an isomer thereof), and R is represented by the formula:

—(CH₂)_nCH═CH₂

where n is an integer from 2 to 18, preferably 6 to 18, preferably 6 to 12, preferably 6. In any embodiment of the invention described herein, particularly useful AVTAs include, but are not limited to, tri(but-3-en-1-yl)aluminum, tri(pent-4-en-1-yl)aluminum, tri(oct-7-en-1-yl)aluminum, tri(non-8-en-1-yl)aluminum, tri(dec-9-en-1-yl)aluminum, dimethyl(oct-7-en-1-yl)aluminum, diethyl(oct-7-en-1-yl)aluminum, dibutyl(oct-7-en-1-yl)aluminum, diisobutyl(oct-7-en-1-yl)aluminum, diisobutyl(non-8-en-1-yl)aluminum, diisobutyl(dec-9-en-1-yl)aluminum, diisobutyl(dodec-11-en-1-yl)aluminum, isobutyl-di(oct-7-en-1-yl)-aluminum, isobutyl-di(dec-9-en-1-yl)-aluminum, isobutyl-di(non-8-en-i-yl)-aluminum, isobutyl-di(hept-6-en-1-yl)-aluminum and the like. Mixtures of one or more AVTAs may also be used. In some embodiments of the invention, isobutyl-di(oct-7-en-1-yl)-aluminum, isobutyl-di(dec-9-en-1-yl)-aluminum, isobutyl-di(non-8-en-1-yl)-aluminum, isobutyl-di(hept-6-en-1-yl)-aluminum are preferred.

Useful aluminum vinyl transfer agents include organoaluminum compound reaction products between aluminum reagent (AlR^a₃) and an alkyl diene. Suitable alkyl dienes include those that have two “alpha olefins,” as described above, at two termini of the carbon chain. The alkyl diene can be a straight chain or branched alkyl chain and substituted or unsubstituted. Exemplary alkyl dienes include but are not limited to, for example, 1,3-butadiene, 1,4-pentadiene, 1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, 1,9-decadiene, 1,10-undecadiene, 1,11-dodecadiene, 1,12-tridecadiene, 1,13-tetradecadiene, 1,14-pentadecadiene, 1,15-hexadecadiene, 1,16-heptadecadiene, 1,17-octadecadiene, 1,18-nonadecadiene, 1,19-eicosadiene, 1,20-heneicosadiene, etc. Exemplary aluminum reagents include triisobutylaluminum, diisobutylaluminumhydride, isobutylaluminumdihydride and aluminum hydride (AlH₃).

In any embodiment of the invention described herein, R″ is butenyl, pentenyl, heptenyl, or octenyl. In some embodiments R″ is preferably octenyl.

In any embodiment of the invention described herein, R′ is methyl, ethyl, propyl, isobutyl, or butyl. In any embodiment of the invention described herein, R′ is isobutyl.

In any embodiment of the invention described herein, v is about 2, or v is 2.

In any embodiment of the invention described herein, v is about 1, or v is 1, preferably from about 1 to about 2.

In any embodiment of the invention described herein, v is an integer or a non-integer, preferably v is from 1.1 to 2.9, from about 1.5 to about 2.7, e.g., from about 1.6 to about 2.4, from about 1.7 to about 2.4, from about 1.8 to about 2.2, from about 1.9 to about 2.1 and all ranges there between.

In preferred embodiments of the invention described herein, R′ is isobutyl and each R″ is octenyl, preferably R′ is isobutyl, each R″ is octenyl, and v is from 1.1 to 2.9, from about 1.5 to about 2.7, e.g., from about 1.6 to about 2.4, from about 1.7 to about 2.4, from about 1.8 to about 2.2, from about 1.9 to about 2.1.

The amount of v (the aluminum alkenyl) is described using the formulas: (3−v)+v=3, and Al(R′)_3-v(R″)_vwhere R″ is a hydrocarbenyl group containing 4 to 20 carbon atoms having an allyl chain end, R′ is a hydrocarbyl group containing 1 to 30 carbon atoms, and v is 0.1 to 3 (preferably 1.1 to 3). This formulation represents the observed average of organoaluminum species (as determined by ¹H NMR) present in a mixture, which may include any of Al(R′)₃, Al(R′)₂(R″), Al(R′)(R″)₂, and Al(R″)₃. ¹H NMR spectroscopic studies are performed at room temperature using a Bruker 400 MHz NMR. Data is collected using samples prepared by dissolving 10-20 mg the compound in 1 mL of C₆D₆. Samples are then loaded into 5 mm NMR tubes for data collection. Data is recorded using a maximum pulse width of 45°, 8 seconds between pulses and signal averaging either 8 or 16 transients. The spectra are normalized to protonated tetrachloroethane in the C₆D₆. The chemical shifts (6) are reported as relative to the residual protium in the deuterated solvent at 7.15 ppm.

In still another aspect, the aluminum vinyl-transfer agent has less than 50 wt % dimer present, based upon the weight of the AVTA, preferably less than 40 wt %, preferably less than 30 wt %, preferably less than 20 wt %, preferably less than 15 wt %, preferably less than 10 wt %, preferably less than 5 wt %, preferably less than 2 wt %, preferably less than 1 wt %, preferably 0 wt % dimer. Alternately dimer is present at from 0.1 to 50 wt %, alternately 1 to 20 wt %, alternately at from 2 to 10 wt %. Dimer is the dimeric product of the alkyl diene used in the preparation of the AVTA. The dimer can be formed under certain reaction conditions, and is formed from the insertion of a molecule of diene into the Al—R bond of the AVTA, followed by beta-hydride elimination. For example, if the alkyl diene used is 1,7-octadiene, the dimer is 7-methylenepentadeca-1,14-diene. Similarly, if the alkyl diene is 1,9-decadiene, the dimer is 9-methylenenonadeca-1,18-diene.

Useful compounds can be prepared by combining an aluminum reagent (such as alkyl aluminum) having at least one secondary alkyl moiety (such as triisobutylaluminum) and/or at least one hydride, such as a dialkylaluminum hydride, a monoalkylaluminum dihydride or aluminum trihydride (aluminum hydride, AlH₃) with an alkyl diene and heating to a temperature that causes release of an alkylene byproduct. The use of solvent(s) is not required. However, non-polar solvents can be employed, such as, as hexane, pentane, toluene, benzene, xylenes, and the like, or combinations thereof.

In an embodiment of the invention, the AVTA is free of coordinating polar solvents such as tetrahydrofuran and diethylether.

After the reaction is complete, solvent if, present can be removed and the product can be used directly without further purification.

The AVTA to catalyst complex equivalence ratio can be from about 100:1 to 500,000:1. More preferably, the molar ratio of AVTA to catalyst complex is greater than 125:1, alternately greater than 145:1, alternately greater than 150:1.

The metal hydrocarbenyl chain transfer agent may be represented by the formula: E[Al(R′)_2-v(R)_v]₂wherein E is a group 16 element (such as O or S, preferably O); each R′, independently, is a C₁to C₃₀hydrocarbyl group (such as a C₁to C₂₀alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, or an isomer thereof); each R″, independently, is a C₄to C₂₀hydrocarbenyl group having an allyl chain end (such as a C₁to C₂₀alkenyl group, preferably methenyl, ethenyl, propenyl, butenyl, pentenyl, heptenyl, octenyl, nonenyl, decenyl, undecenyl, dodecenyl, or an isomer thereof); v is from 0.01 to 3 (such as 1 or 2).

In another embodiment of the invention, the metal hydrocarbenyl chain transfer agent is an alumoxane formed from the hydrolysis of the AVTA. Alternatively, the alumoxane can be formed from the hydrolysis of the AVTA in combination with other aluminum alkyl(s). The alumoxane component is an oligomeric compound which is not well characterized, but can be represented by the general formula (R—Al—O)_mwhich is a cyclic compound, or may be R′(R—Al—O)_m—AlR′₂which is a linear compound where R′ is as defined above and at least one R′ is the same as R (as defined above), and m is from about 4 to 25, with a range of 13 to 25 being preferred. Most preferably all R′ are R. An alumoxane is generally a mixture of both the linear and cyclic compounds.

Supports

The complexes described herein may be supported (with or without an activator and with or without a transfer agent) by any method effective to support other coordination catalyst systems, effectively meaning that the catalyst so prepared can be used for polymerizing olefin(s) in a heterogeneous process. The catalyst precursor, activator, optional transfer agent, co-activator if needed, suitable solvent, and support may be added in any order or simultaneously. Typically, the complex, activator, and optional transfer agent may be combined in solvent to form a solution. Then the support is added, and the mixture is stirred for 1 minute to 10 hours. The total solution volume may be greater than the pore volume of the support, but some embodiments limit the total solution volume below that needed to form a gel or slurry (about 90% to 400%, preferably about 100% to 200% of the pore volume). After stirring, the residual solvent is removed under vacuum, typically at ambient temperature and over 10-16 hours. But greater or lesser times and temperatures are possible.

The complex may also be supported absent the activator, and in that case, the activator (and co-activator if needed) is added to a polymerization process' liquid phase. Additionally, two or more different complexes may be placed on the same support. Likewise, two or more activators or an activator and co-activator may be placed on the same support. Likewise the transfer agent may be added to the polymerization reaction separately from the supported catalyst complex and/or activator.

Suitable solid particle supports are typically comprised of polymeric or refractory oxide materials, each being preferably porous. Preferably, any support material that has an average particle size greater than 10 μm is suitable for use in this invention. Various embodiments select a porous support material, such as for example, talc, inorganic oxides, inorganic chlorides, for example magnesium chloride and resinous support materials such as polystyrene polyolefin or polymeric compounds or any other organic support material and the like. Some embodiments select inorganic oxide materials as the support material including Group-2, -3, -4, -5, -13, or -14 metal or metalloid oxides. Some embodiments select the catalyst support materials to include silica, alumina, silica-alumina, and their mixtures. Other inorganic oxides may serve either alone or in combination with the silica, alumina, or silica-alumina. These are magnesia, titania, zirconia, and the like. The support can optionally double as the activator component; however, an additional activator may also be used.

The support material may be pre-treated by any number of methods. For example, inorganic oxides may be calcined, chemically treated with dehydroxylating agents such as aluminum alkyls and the like, or both.

As stated above, polymeric carriers will also be suitable in accordance with the invention, see, for example, the descriptions in WO 95/15815 and U.S. Pat. No. 5,427,991. The methods disclosed may be used with the catalyst complexes, activators or catalyst systems of this invention to adsorb or absorb them on the polymeric supports, particularly if made up of porous particles, or may be chemically bound through functional groups bound to or in the polymer chains.

Useful supports typically have a surface area of from 10-700 m²/g, a pore volume of 0.1-4.0 cc/g and an average particle size of 10-500 μm. Some embodiments select a surface area of 50-500 m2/g, a pore volume of 0.5-3.5 cc/g, or an average particle size of 20-200 am. Other embodiments select a surface area of 100-400 m2/g, a pore volume of 0.8-3.0 cc/g, and an average particle size of 30-100 μm. Useful supports typically have a pore size of 10-1000 Angstroms, alternatively 50-500 Angstroms, or 75-350 Angstroms.

The catalyst complexes described herein are generally deposited on the support at a loading level of 10-100 micromoles of complex per gram of solid support; alternately 20-80 micromoles of complex per gram of solid support; or 40-60 micromoles of complex per gram of support. However, greater or lesser values may be used provided that the total amount of solid complex does not exceed the support's pore volume.

Polymerization

Invention catalyst complexes are useful in polymerizing unsaturated monomers conventionally known to undergo coordination-catalyzed polymerization such as solution, slurry, gas-phase, and high-pressure polymerization. Typically, one or more of the complexes described herein, one or more activators, one or more transfer agents (such as an aluminum vinyl transfer agent) and three or more monomers (e.g. at least ethylene, propylene and diene monomers) are contacted to produce polymer. The complexes may be supported and, as such, will be particularly useful in the known, fixed-bed, moving-bed, fluid-bed, slurry, gas phase, solution, or bulk operating modes conducted in single, series, or parallel reactors.

One or more reactors in series or in parallel may be used in the present invention.

The complexes, activator, transfer agent, and, when required, co-activator, may be delivered as a solution or slurry, either separately to the reactor, activated in-line just prior to the reactor, or pre-activated and pumped as an activated solution or slurry to the reactor. Polymerizations are carried out in either single reactor operation, in which monomer, comonomers, catalyst/activator/co-activator, optional scavenger, and optional modifiers are added continuously to a single reactor or in series reactor operation, in which the above components are added to each of two or more reactors connected in series. The catalyst components can be added to the first reactor in the series. The catalyst component may also be added to both reactors, with one component being added to the first reaction and another component to other reactors. In one preferred embodiment, the complex is activated in the reactor in the presence of olefin and transfer agent.

In a particularly preferred embodiment, the polymerization process is a continuous process.

Polymerization process used herein typically comprises contacting one or more alkene monomers with the complexes, activators and transfer agents described herein. For purpose of this invention alkenes are defined to include multi-alkenes (such as dialkenes) and alkenes having just one double bond. Polymerization may be homogeneous (solution or bulk polymerization) or heterogeneous (slurry—in a liquid diluent, or gas phase—in a gaseous diluent). In the case of heterogeneous slurry or gas phase polymerization, the complex and activator may be supported. Silica is useful as a support herein. Chain transfer agents (such as hydrogen or diethyl zinc) may be used in the practice of this invention.

The present polymerization processes may be conducted under conditions preferably including a temperature of about 30° C. to about 200° C., preferably from 60° C. to 195° C., preferably from 75° C. to 190° C. The process may be conducted at a pressure of from 0.05 to 1500 MPa. In a preferred embodiment, the pressure is between 1.7 MPa and 30 MPa, or in another embodiment, especially under supercritical conditions, the pressure is between 15 MPa and 1500 MPa.

In a preferred embodiment, the present polymerization processes may be conducted under conditions preferably including a temperature of from 85° C. to 190° C., alternately from 90° C. to 190° C., alternately from 95° C. to 190° C., alternately from 100° C. to 190° C.

If branching (such a g′_visof less than 0.90) is desired in the polymer product, then, among other things, one may increase the moles of metal hydrocarbenyl chain transfer agent added to the reactor relative to the amount of polymer produced (such as grams of polymer/mols of AVTA being less than 500,000; 400,000 or less; 200,000 or less; 100,000 or less; 50,000 or less; 25,000 or less; 10,000 or less), and/or increase the temperature of the polymerization reaction (such as above 80° C.), and/or increase the solids content in the polymerization reaction mass (such as 10 weight % or more, based on the weight of the components entering the reactor, alternately 11 wt % or more, alternately 12 wt % or more), and/or increase the residence time of the polymerization (such as 10 minutes or more, alternately 11 minutes or more, alternately 12 minutes or more, alternately 12.5 minutes or more). Likewise, if a more linear polymer is desired (such as a g′_visof more than 0.95), then, among other things, one may reduce the moles of metal hydrocarbenyl chain transfer agent added to the reactor relative to the amount of polymer produced (such as grams of polymer/mols of AVTA being 500,000 or more), and/or reduce the temperature of the polymerization reaction (such as 80° C. or less), and/or reduce the solids content in the polymerization reaction mass such as 10 volume % or less), and/or reduce the residence time of the polymerization (such as 10 minutes or less). One of ordinary skill in the art will readily appreciate that 1, 2, 3 or 4 of the above conditions may be varied above or below the suggested conditions above to obtain a desired result. For example a lower catalyst/AVTA molar ratio can be used if the catalyst activity is higher.

Monomers

Monomers useful herein include olefins having from 2 to 40 carbon atoms, alternately 2 to 12 carbon atoms (preferably ethylene, propylene, butylene, pentene, hexene, heptene, octene, nonene, decene, and dodecene) and, polyenes (such as dienes). Particularly preferred monomers include ethylene, propylene, and diene monomers.

The catalyst systems described herein are also particularly effective for the polymerization of ethylene and propylene in combination with at least one other diolefinically unsaturated monomer, such as a C₄to C₂₀diene, and particularly a C₃to C₁₂diene.

Examples of preferred α-olefins that may be combined with the ethylene, propylene, and diene monomers include: butene-1, pentene-1, hexene-1, heptene-1, octene-1, nonene-1, decene-1, dodecene-1, 4-methylpentene-1, 3-methylpentene-1, 3, 5, 5-trimethylhexene-1, and 5-ethylnonene-1.

The monomer mixture preferably comprises one or more dienes at up to 10 wt %, such as from 0.00001 to 1.0 wt %, for example from 0.002 to 0.5 wt %, such as from 0.003 to 0.2 wt %, based upon the monomer mixture. In some embodiments 500 ppm to 1 ppm of diene is added to the polymerization, alternately 400 ppm to 1 ppm, alternately 300 ppm to 1 ppm. In other embodiments, at least 50 ppm of diene is added to the polymerization, or 100 ppm or more, or 150 ppm or more.

Preferred diene monomers useful in this invention include any hydrocarbon structure, preferably C₄to C₃₀, having at least two unsaturated bonds, wherein at least two of the unsaturated bonds are readily incorporated into a polymer by either a stereospecific or a non-stereospecific catalyst(s). It is further preferred that the diene monomers be selected from alpha, omega-diene monomers (i.e. di-vinyl monomers). More preferably, the diene monomers are linear di-vinyl monomers, most preferably those containing from 4 to 30 carbon atoms. Examples of preferred dienes include butadiene, pentadiene, hexadiene, heptadiene, octadiene, nonadiene, decadiene, undecadiene, dodecadiene, tridecadiene, tetradecadiene, pentadecadiene, hexadecadiene, heptadecadiene, octadecadiene, nonadecadiene, icosadiene, heneicosadiene, docosadiene, tricosadiene, tetracosadiene, pentacosadiene, hexacosadiene, heptacosadiene, octacosadiene, nonacosadiene, triacontadiene, particularly preferred dienes include 1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, 1,9-decadiene, 1,10-undecadiene, 1,11-dodecadiene, 1,12-tridecadiene, 1,13-tetradecadiene, and low molecular weight polybutadienes (Mw less than 1000 g/mol). Preferred cyclic dienes include cyclopentadiene, vinylnorbornene, norbornadiene, ethylidene norbornene, divinylbenzene, dicyclopentadiene or higher ring containing diolefins with or without substituents at various ring positions.

Particularly preferred examples of useful dienes include: 5-ethylidene-2-norbornene, 1,4-hexadiene, 1,5-heptadiene, 6-methyl-1,6-heptadiene, 1,6-octadiene, 7-methyl-1,7-octadiene, 1,8-decadiene, and 9-methyl-1,9-decadiene.

In a preferred embodiment, the diene monomer comprises two different diene monomers, such as ethylidene norbornene and vinyl norbornene.

Where olefins are used that give rise to short chain branching, such as propylene, the catalyst systems may, under appropriate conditions, generate stereoregular polymers or polymers having stereoregular sequences in the polymer chains.

In a preferred embodiment, the catalyst systems described herein are used in any polymerization process described above to produce propylene-ethylene-diene terpolymers.

Scavengers

In some embodiments, when using the complexes described herein, particularly when they are immobilized on a support, the catalyst system will additionally comprise one or more scavenging compounds. Here, the term scavenging compound means a compound that removes polar impurities from the reaction environment. These impurities adversely affect catalyst activity and stability. Typically, the scavenging compound will be an organometallic compound such as the Group-13 organometallic compounds of U.S. Pat. No. 5,153,157; U.S. Pat. No. 5,241,025; WO 1991/09882; WO 1994/03506; WO 1993/14132; and that of WO 1995/07941. Exemplary compounds include triethyl aluminum, triethyl borane, tri-iso-butyl aluminum, methyl alumoxane, iso-butyl alumoxane, tri-n-octyl aluminum, bis(diisobutylaluminum)oxide, modified methylalumoxane. (Useful modified methylalumoxane include cocatalyst type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylalumoxane type 3A) and those described in U.S. Pat. No. 5,041,584). Those scavenging compounds having bulky or C₆-C₂₀linear hydrocarbyl substituents connected to the metal or metalloid center usually minimize adverse interaction with the active catalyst. Examples include triethylaluminum, but more preferably, bulky compounds such as tri-iso-butyl aluminum, tri-iso-prenyl aluminum, and long-chain linear alkyl-substituted aluminum compounds, such as tri-n-hexyl aluminum, tri-n-octyl aluminum, or tri-n-dodecyl aluminum. When alumoxane is used as the activator, any excess over that needed for activation will scavenge impurities and additional scavenging compounds may be unnecessary. Alumoxanes also may be added in scavenging quantities with other activators, e.g., methylalumoxane, [Me₂HNPh]⁺[B(pfp)₄]⁻ or B(pfp)₃(perfluorophenyl=pfp=C₆F₅).

In embodiments, the transfer agent, such as the aluminum vinyl transfer agent, may also function as a scavenger.

In a preferred embodiment, two or more catalyst complexes as described herein are combined with a chain transfer agent, such as diethyl zinc or tri-n-octylaluminum, in the same reactor with monomer. Alternately, one or more complexes are combined with another catalyst (such as a metallocene) and a chain transfer agent, such as diethyl zinc and/or tri-n-octylaluminum, in the same reactor with monomer.

Polymer Products

While the molecular weight of the polymers produced herein is influenced by reactor conditions including temperature, monomer concentration and pressure, the presence of chain terminating agents and the like, the copolymer products produced by the present process may have an Mw of about 200,000 to about 2,000,000 g/mol, alternately of about 250,000 to about 1,000,000 g/mol, or alternately of about 300,000 to about 900,000 g/mol, as determined by Gel Permeation Chromatography. Preferred polymers produced herein are copolymers of at least 30 wt % propylene. In a preferred embodiment, the ethylene and diene comonomer(s) are present at up to 70 mol %, preferably from 1 to 65 mol %, preferably 5 to 60 mol %.

Preferred polymers produced herein comprise from about 98.9 to 30 wt % propylene (preferably from 90 to 35 wt %, preferably from 80 to 40 wt %), from 1 to 70 wt % ethylene (preferably from 5 to 68 wt %, preferably from 10 to 65 wt %), from 0.1 to 20 wt % diene monomer (preferably from 0.5 to 18 wt %, preferably from 1 to 18 wt %, preferably from 2 to 15 wt %).

The polymers produced by the process of the invention can be used in a wide variety of products and end-use applications. The ethylene-propylene-diene terpolymers produced can comprise include isotactic polypropylene, atactic polypropylene and random, block or impact copolymers.

The copolymers of embodiments of the invention may have an M_n(number-average molecular weight) value of 12,500 g/mol or more, typically from 12,500 to 1,000,000, or between from 700 to 300,000 g/mol. Additionally, copolymer of embodiments of the invention will comprise a molecular weight distribution (Mw/Mn) of 3.0 or more, alternately 3.3 or more, alternately 3.5 or more.

Typically, polymer produced herein has an Mw of 250,000 up to 2,000,000 g/mol and a g′_visof 0.90 or less, or 0.88 or less, or 0.85 or less.

Preferably, the polymer produced herein is gel-free. Presence of gel can be detected by dissolving the material in xylene at xylene's boiling temperature (140° C.) and measuring the amount of gel present (See ASTM D 5492, except that 140° C. is used rather than 20° C.). Gel-free product should be dissolved in the xylene. In one embodiment, the branched modifier has 5 wt % or less (preferably 4 wt % or less, preferably 3 wt % or less, preferably 2 wt % or less, preferably 1 wt % or less, preferably 0 wt %) of xylene insoluble material.

In particularly useful embodiments of the invention, propylene-ethylene-diene terpolymers are produced herein: a) have a g′_visof less than 0.90 (preferably 0.88 or less, preferably 0.85 or less); b) are preferably essentially gel free (such as 5 wt % or less of xylene insoluble material); c) have an Mw of 250,000 g/mol or more (preferably 300,000 g/mol or more, preferably 350,000 g/mol or more); d) have a Mw/Mn of greater than 3.0 (preferably 3.3 or more, preferably 3.5 or more); and e) have an Mz of 850,000 g/mol or more (preferably 870,000 g/mol or more, preferably 890,000 g/mol or more).

This invention relates to branched ethylene-propylene-diene monomer based copolymer modifiers comprising from about 98.9 to 30 wt % propylene, from 1 to 70 wt % ethylene, from 0.5 to 20 wt % diene monomer, and a remnant of the metal hydrocarbenyl chain transfer agent, wherein said branched copolymer based polymer modifier preferably has a g′_visof less than 0.90 (preferably less than 0.85) and a complex viscosity of at least 5000 Pa·s measured at 0.1 rad/sec and a temperature of 190° C.

This invention further relates to novel branched propylene based copolymers comprising from about 98.9 to 30 wt % propylene (preferably from 90 to 35 wt % propylene), from 1 to 70 wt % ethylene (preferably from 5 to 65 wt % ethylene), from 0.5 to 20 wt % diene monomer (preferably from 1 to 18 wt % diene, alternatively from 2 to 15 wt % diene), and a remnant of the metal hydrocarbenyl chain transfer agent (preferably from 0.001 to 10 mol %, alternatively from 0.01 to 5 mol %, alternatively 0.01 to 2 mol %, alternatively 0.01 to 1 mol %), wherein said branched copolymer: a) has a g′_visof less than 0.90 (preferably 0.88 or less, alternatively 0.86 or less, alternatively 0.85 or less,); b) is essentially gel free (such as 5 wt % or less of xylene insoluble material, alternatively 4 wt % or less, alternatively 3 wt % or less, alternatively 2 wt % or less, alternatively 1 wt % or less, alternatively 0 wt %); c) has a Mw of 250,000 g/mol or more (preferably 270,000 or more, alternatively 290,000 g/mol or more, alternatively 3000,000 g/mol or more); d) has a Mz of 850,000 g/mol or more (preferably 870,000 or more, alternatively 890,000 g/mol or more); and e) has a Mw/Mn of 3.0 or more (preferably 3.3 or more, alternatively 3.5 more, alternatively from 3.0 to 10).

This invention also relates to novel branched copolymers having a complex viscosity of at least 500 Pa·s (preferably from 1000 to 150,000 Pa·s, preferably from 5,000 to 125,000 Pa·s, preferably from 10,000 to 100,000 Pa·s) measured at 0.1 rad/sec and a temperature of 190° C.

This invention further relates to novel branched ethylene-propylene-diene copolymers comprising from about 70 to 30 wt % propylene (preferably from 60 to 35 wt % propylene, alternatively from 55 to 40 wt % propylene, alternatively from 55 to 45 wt % propylene), from 30 to 70 wt % ethylene (preferably from 40 to 65 wt % ethylene, alternatively from 45 to 60 wt % ethylene, alternatively from 45 to 55 wt % ethylene), from 1 to 20 wt % diene monomer (preferably from 1 to 18 wt % diene, alternatively from 2 to 15 wt % diene, alternatively from 4 to 10 wt % diene), and a remnant of the metal hydrocarbenyl chain transfer agent (preferably from 0.001 to 10 mol %, alternatively from 0.01 to 5 mol %, alternatively 0.01 to 2 mol %, alternatively 0.01 to 1 mol %), wherein said branched propylene based polymer modifier preferably has a g′_visof less than 0.90 (alternatively, 0.88 or less, alternatively 0.85 or less,); and a complex viscosity of at least 500 Pa·s (preferably from 1000 to 150,000 Pa·s, preferably from 5,000 to 125,000 Pa·s, preferably from 10,000 to 100,000 Pa·s) measured at 0.1 rad/sec and a temperature of 190° C.

End Uses

The polymers of this invention may be used alone or may be blended and/or coextruded with any other polymer. Non-limiting examples of other polymers include linear low density polyethylenes, elastomers, plastomers, high pressure low density polyethylene, high density polyethylenes, isotactic polypropylene, ethylene propylene copolymers and the like.

Articles made using polymers produced herein may include, for example, molded articles (such as containers and bottles, e.g., household containers, industrial chemical containers, personal care bottles, medical containers, fuel tanks, and storageware, toys, sheets, pipes, tubing) films, non-wovens, and the like. It should be appreciated that the list of applications above is merely exemplary, and is not intended to be limiting.

In particular, polymers produced by the process of the invention and blends thereof are useful in such foaming operations as weather seals and weather strips.

EXPERIMENTAL
Aluminum Vinyl Transfer Agent

All manipulations were performed under an inert atmosphere using glove box techniques unless otherwise stated. Benzene-d₆(Cambridge Isotopes) (Sigma Aldrich) was degassed and dried over 3 Å molecular sieves prior to use. CDCl₃(Deutero GmbH) was used as received.

Diisobutylaluminum hydride (DIBAL-H) was purchased from Akzo Nobel Surface Chemistry LLC and used as received. 1,7-octadiene and 1,9-decadiene were purchased from Sigma Aldrich and purified by the following procedure prior to use. The diene was purged under nitrogen for 30 minutes and then this was stored over 3 Å molecular sieves for overnight. Further this was stirred with NaK (sodium-potassium alloy) for overnight and then filtered through basic alumina column prior to use.

Example 1: Preparation of diisobutyl(oct-7-en-1-yl)aluminum, ⁱBu₂Al(Oct=) (AVTA1)

A neat 1,7-octadiene (16.53 g, 150 mmol) was added drop wise to diisobutylaluminum hydride (3.56 g, 25 mmol) at room temperature over a period of 5 minutes. The reaction mixture was either stirred at 45° C. for overnight. The excess 1,7-octadiene from the reaction mixture was removed under the flow of dry nitrogen at room temperature. The residual 1,7-octadiene was then removed in vacuo for 30 minutes to obtain a colorless viscous oil of diisobutyl(oct-7-en-1-yl) aluminum, iBu₂Al(Oct=) (6.055 g, 96%). The product formation was confirmed by ¹H NMR spectroscopy and based on the relative integration the molecular formula was assigned as (C₄H₉)_2.09Al(C₈H₅)_0.91. ¹H NMR (400 MHz, benzene-d₆): δ=5.78 (m, 1H, ═CH), 5.01 (m, 2H, ═CH₂), 1.95 (m, 4H, —CH₂), 1.54 (m, 2H, ⁱBu-CH), 1.34 (m, 6H, —CH₂), 1.04 (d, 12H, ⁱBu-CH₃), 0.49 (t, 2H, Al—CH₂), 0.27 (d, 4H, ⁱBu-CH₂) ppm.

Example 2: Preparation of Isobutyldi(oct-7-en-1-yl)aluminum, ⁱBuAl(Oct=)₂(AVTA2)
Example 2A

A neat 1,7-octadiene (22.91 g, 207.9 mmol) was added drop wise to diisobutylaluminum hydride (2.61 g, 18.4 mmol) at room temperature over 5 minutes. The resulting mixture was stirred under reflux at 110° C. for 60 minutes and then continuously stirring at 70° C. for overnight. The excess 1,7-octadiene from the reaction mixture was removed under the flow of dry nitrogen at room temperature. The residual 1,7-octadiene was then removed in vacuum to obtain a colorless viscous oil of isobutyldi(oct-7-en-1-yl)aluminum, iBuAl(Oct=)₂(5.53 g, 97%). The product formation was confirmed by ¹H NMR and based on the relative integration the molecular formula of was assigned as (C₄H₉)_0.95Al(C₈H₁₅)_2.05. ¹H NMR (400 MHz, benzene-d₆): δ=5.81 (m, 2H, ═CH), 5.05 (m, 4H, ═CH₂), 2.03 (m, 8H, —CH₂), 1.59 (m, 1H, ⁱBu-CH), 1.38 (m, 12H, —CH₂), 1.09 (d, 6H, ⁱBu-CH₃), 0.51 (t, 4H, Al—CH₂), 0.31 (d, 2H, ⁱBu-CH₂) ppm.

Example 2B

A neat 1,7-octadiene (34.86 g, 316.3 mmol) was added drop wise to diisobutylaluminum hydride (3.98 g, 27.99 mmol) at room temperature over 5 minutes. The resulting mixture was stirred under reflux at 110° C. for 60 minutes and then continuously stirring at 70° C. for overnight. The excess 1,7-octadiene from the reaction mixture was removed under the flow of dry nitrogen at room temperature. The residual 1,7-octadiene was then removed in vacuum to obtain a colorless viscous oil of isobutyldi(oct-7-en-1-yl)aluminum, iBuAl(Oct=)₂(8.041 g, 94%). The product formation was confirmed by ¹H NMR and based on the relative integration the molecular formula of was assigned as (C₄H₉)_1.04Al(C₈H₁₅)_1.96.

For AVTA2, 0.446 g of Example 2A and 7.756 g of Example 2B were blended together to make AVTA2.

Example 3: Preparation of Isobutyldi(oct-7-en-1-yl)aluminum, ⁱBuAl(Oct=)₂(AVTA3)

1,7-Octadiene (250 mL, 1.69 mol) was loaded into a round-bottomed flask. Diisobutylaluminum hydride (27.4 mL, 0.153 mol) was added dropwise over 20 minutes. The mixture was then placed into a metal block maintained at 117° C. After about 20 minutes the mixture reached 107° C. and this temperature was maintained for 125 minutes. The mixture was then cooled to ambient temperature and the volatiles were removed under a stream of nitrogen to afford a nearly colorless oil. The oil was placed under reduced pressure (ca. 60 mTorr) and warmed to 50° C. for 30 minutes to remove any trace 1,7-octadiene. The yield was 54.0 g. H-NMR spectroscopic data indicated that the product had the average formula of Al(iBu)_0.9(octenyl)_2.1with a small amount (ca. 0.2 molar equivalents) of vinylidene containing byproduct, that may be formed by the insertion of 1,7-octadiene into an Al-octenyl bond followed by beta hydride elimination.

Example 4: Preparation of Isobutyldi(dec-9-en-1-yl)aluminum, ⁱBuAl(Dec=)₂(AVTA4)

1,9-Decadiene (500 mL, 2.71 mol) was loaded into a round-bottomed flask. Diisobutylaluminum hydride (30.2 mL, 0.170 mol) was added dropwise over 15 minutes. The mixture was then placed in a metal block maintained at 110° C. After 30 minutes the solution had stabilized at a temperature of 104° C. The mixture was kept at this temperature for an additional 135 minutes at which time H-NMR spectroscopic data indicated that the reaction had progressed to the desired amount. The mixture was cooled to ambient temperature. The excess 1,9-decadiene was removed by vacuum distillation at 44° C./120 mTorr over a 2.5 hours. The product was further distilled at 50° C./120 mTorr for an additional hour to ensure complete removal of all 1,9-decadiene. The isolated product was a clear colorless oil. The yield was 70.9 g. H-NMR spectroscopic data indicated an average formula of Al(iBu)_0.9(decenyl)_2.1, with a small amount (ca. 0.2 molar equivalents) of vinylidene containing byproduct, that may be formed by the insertion of 1,9-decadiene into an Al-octenyl bond followed by beta hydride elimination.

Activator and Catalyst Complexes

[Image Omitted]

Complex 1 was prepared as described in U.S. Pat. No. 9,290,519. The activator used was dimethylanilinium tetrakis(pentafluorophenyl)borane (available from Albemarle Corp. or Boulder Scientific).

[Image Omitted]

Complex 2 is 2-(8-anilino-5,6,7,8-tetrahydronaphthalen-1-yl)-N-(2,6-diisopropylphenyl) quinolin-8-amido hafnium dimethyl, was prepared as described below. The activator used was dimethylanilinium tetrakis(pentafluorophenyl)borane (available from Albemarle Corp. or Boulder Scientific).

8-(2,6-Diisopropylphenylamino)quinolin-2(1H)-one

To a suspension of NaH (5.63 g of 60 wt % in mineral oil, 140 mmol) in tetrahydrofuran (1000 mL) was added 8-bromoquinolin-2(1H)-one (30.0 g, 134 mmol) in small portions at 0° C. The obtained reaction mixture was warmed to room temperature, stirred for 30 min, and then cooled to 0° C. Then t-butyldimethylsilylchloride (20.2 g, 134 mmol) was added in one portion. This mixture was stirred for 30 min at room temperature and then poured into water (1 L). The protected 8-bromoquinolin-2(1H)-one was extracted with diethyl ether (3×400 mL). The combined extracts were dried over Na₂SO₄and then evaporated to dryness. Yield 45.2 g (quant., 99% purity by GC/MS) of a dark red oil. To a solution of 2,6-diisopropylaniline (27.7 mL, 147 mmol) and toluene (1.5 L) was added n-butyllithium (60.5 mL, 147 mmol, 2.5 M in hexanes) at room temperature. The obtained suspension was heated briefly to 100° C. and then cooled to room temperature. To the reaction mixture was added Pd₂(dba)₃(dba=dibenzylideneacetone) (2.45 g, 2.68 mmol) and XPhos (XPhos=2-Dicyclohexylphosphino-2′,4′,6′-triisopropylbiphenyl) (2.55 g, 5.36 mmol) followed by the addition of the protected 8-bromoquinolin-2(1H)-one (45.2 g, 134 mmol). The obtained dark brown suspension was heated at 60° C. until lithium salt precipitate disappeared (ca. 30 min). The resulting dark red solution was quenched by addition of water (100 mL), and the organic layer was separated, dried over Na₂SO₄and then evaporated to dryness. The obtained oil was dissolved in a mixture of dichloromethane (1000 mL) and methanol (500 mL), followed by an addition of 12 M HCl (50 mL). The reaction mixture was stirred at room temperature for 3 h, then poured into 5% K₂CO₃(2 L). The product was extracted with dichloromethane (3×700 mL). The combined extracts were dried over Na₂SO₄, filtered, and then evaporated to dryness. The resulting solid was triturated with n-hexane (300 mL), and the obtained suspension collected on a glass frit. The precipitate was dried in vacuum. Yield 29.0 g (67%) of a marsh-green solid. Anal. calc. for C₂₁H₂₄N₂O: C, 78.71; H, 7.55; N, 8.74. Found: C, 79.00; H, 7.78; N, 8.50. ¹H NMR (CDCl₃): δ 13.29 (br.s, 1H), 7.80-7.81 (d, 1H, J=9.5 Hz), 7.35-7.38 (m, 1H), 7.29-7.30 (m, 3H), 6.91-6.95 (m, 2H), 6.58-6.60 (d, 1H, J=9.5 Hz), 6.27-6.29 (m, 1H), 3.21 (sept, 2H, J=6.9 Hz), 1.25-1.26 (d, 6H, J=6.9 Hz), 1.11-1.12 (d, 6H, J=6.9 Hz).

2-Chloro-N-(2,6-diisopropylphenyl)quinolin-8-amine

29.0 g (90.6 mmol) of 8-(2,6-diisopropylphenylamino)quinolin-2(1H)-one was added to 400 mL of POCl₃in one portion. The resulting suspension was heated for 40 h at 105° C., then cooled to room temperature, and poured into 4000 cm³of a crushed ice. The crude product was extracted with 3×400 mL of diethyl ether. The combined extract was dried over K₂CO₃and then evaporated to dryness. The resulting solid was triturated with 30 mL of cold n-hexane, and the formed suspension was collected on a glass frit. The obtained solid was dried in vacuum. Yield 29.0 g (95%) of a yellow-green solid. Anal. calc. for C₂₁H₂₃N₂Cl: C, 74.43; H, 6.84; N, 8.27. Found: C, 74.68; H, 7.02; N, 7.99. ¹H NMR (CDCl₃): δ 8.04-8.05 (d, 1H, J=8.6 Hz), 7.38-7.39 (d, 1H, J=8.5 Hz), 7.33-7.36 (m, 1H), 7.22-7.27 (m, 4H), 7.04-7.06 (d, 1H, J=8.1 Hz), 6.27-6.29 (d, 1H, J=7.8 Hz), 3.20 (sept, 2H, J=6.9 Hz), 1.19-1.20 (d, 6H, J=6.9 Hz), 1.10-1.11 (d, 6H, J=6.9 Hz).

8-Bromo-1,2,3,4-tetrahydronaphthalen-1-ol

To a mixture of 78.5 g (530 mmol) of 1,2,3,4-tetrahydronaphthalen-1-ol, 160 mL (1.06 mol) of N,N,N′,N′-tetramethylethylenediamine, and 3000 mL of pentane cooled to −20° C. 435 mL (1.09 mol) of 2.5 M ⁿBuLi in hexanes was added dropwise. The obtained mixture was refluxed for 12 h, then cooled to −80° C., and 160 mL (1.33 mol) of 1,2-dibromotetrafluoroethane was added. The obtained mixture was allowed to warm to room temperature and then stirred for 12 h at this temperature. After that, 100 mL of water was added. The resulting mixture was diluted with 2000 mL of water, and the organic layer was separated. The aqueous layer was extracted with 3×400 mL of toluene. The combined organic extract was dried over Na₂SO₄and then evaporated to dryness. The residue was distilled using the Kugelrohr apparatus, b.p. 150-160° C./1 mbar. The obtained yellow oil was dissolved in 100 mL of triethylamine, and the formed solution was added dropwise to a stirred solution of 71.0 mL (750 mmol) of acetic anhydride and 3.00 g (25.0 mmol) of 4-dimethylaminopyridine in 105 mL of triethylamine. The formed mixture was stirred for 5 min, then 1000 mL of water was added, and the obtained mixture was stirred for 12 h. After that, the reaction mixture was extracted with 3×200 mL of ethyl acetate. The combined organic extract was washed with aqueous Na₂CO₃, dried over Na₂SO₄, and then evaporated to dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um, eluent: hexane-ethyl acetate=30:1, vol.). The isolated ester was dissolved in 1500 mL of methanol, 81.0 g (1.45 mol) of KOH was added, and the obtained mixture was heated to reflux for 3 h. The reaction mixture was then cooled to room temperature and poured into 4000 mL of water. The title product was extracted with 3×300 mL of dichloromethane. The combined organic extract was dried over Na₂SO₄and then evaporated to dryness. Yield 56.0 g (47%) of a white crystalline solid. ¹H NMR (CDCl₃): δ 7.38-7.41 (m, 1H, 7-H); 7.03-7.10 (m, 2H, 5.6-H); 5.00 (m, 1H, 1-H), 2.81-2.87 (m, 1H, 4/4′-H), 2.70-2.74 (m, 1H, 4′/4-H), 2.56 (br.s., 1H, OH), 2.17-2.21 (m, 2H, 2,2′-H), 1.74-1.79 (m, 2H, 3,3′-H).

8-Bromo-3,4-dihydronaphthalen-1(2H)-one

To a solution of 56.0 g (250 mmol) of 8-bromo-1,2,3,4-tetrahydronaphthalen-1-ol in 3500 mL of dichloromethane was added 265 g (1.23 mol) of pyridinium chlorochromate (PCC). The resulting mixture was stirred for 5 h at room temperature, then passed through a pad of silica gel 60 (500 mL; 40-63 um), and finally evaporated to dryness. Yield 47.6 g (88%) of a colorless solid. ¹H NMR (CDCl₃): δ 7.53 (m, 1H, 7-H); 7.18-7.22 (m, 2H, 5.6-H); 2.95 (t, J=6.1 Hz, 2H, 4,4′-H); 2.67 (t, J=6.6 Hz, 2H, 2,2′-H); 2.08 (quint, J=6.1 Hz, J=6.6 Hz, 2H, 3,3′-H).

(8-Bromo-1,2,3,4-tetrahydronaphthalen-1-yl)phenylamine

To a stirred solution of 21.6 g (232 mmol) of aniline in 140 mL of toluene was added 10.93 g (57.6 mmol) of TiCl₄over 30 min at room temperature under argon atmosphere. The resulting mixture was stirred for 30 min at 90° C. followed by an addition of 13.1 g (57.6 mmol) of 8-bromo-3,4-dihydronaphthalen-1(2H)-one. This mixture was stirred for 10 min at 90° C., then cooled to room temperature, and poured into 500 mL of water. The product was extracted with 3×50 mL of ethyl acetate. The combined organic extract was dried over Na₂SO₄, evaporated to dryness, and the residue was re-crystallized from 10 mL of ethyl acetate. The obtained crystalline solid was dissolved in 200 mL of methanol, 7.43 g (118 mmol) of NaBH₃CN and 3 mL of acetic acid were added in argon atmosphere. This mixture was heated to reflux for 3 h, then cooled to room temperature, and evaporated to dryness. The residue was diluted with 200 mL of water, and crude product was extracted with 3×100 mL of ethyl acetate. The combined organic extract was dried over Na₂SO₄and evaporated to dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um, eluent: hexane-ethyl acetate-triethylamine=100:10:1, vol.). Yield 13.0 g (75%) of a yellow oil. Anal. Calc. for C₁₆H₁₆BrN: C, 63.59; H, 5.34; N, 4.63. Found: C, 63.82; H, 5.59; N, 4.49. ¹H NMR (CDCl₃): δ 7.44 (m, 1H), 7.21 (m, 2H), 7.05-7.11 (m, 2H), 6.68-6.73 (m, 3H), 4.74 (m, 1H), 3.68 (br.s, 1H, NH), 2.84-2.89 (m, 1H), 2.70-2.79 (m, 1H), 2.28-2.32 (m, 1H), 1.85-1.96 (m, 1H), 1.76-1.80 (m, 1H), 1.58-1.66 (m, 1H).

N-Phenyl-8-(4,4,5,5-tetramethyl-1,3,2-dioxaborolan-2-yl)-1,2,3,4-tetrahydronaphthalen-1-amine

To a solution of 13.0 g (43.2 mmol) of (8-bromo-1,2,3,4-tetrahydronaphthalen-1-yl)phenylamine in 250 mL tetrahydrofuran (THF) was added 17.2 mL (43.0 mmol) of 2.5 M ⁿBuLi at −80° C. Further on, this mixture was stirred for 1 h at this temperature, and 56.0 mL (90.3 mmol) of 1.6 M ^tBuLi in pentane was added. The resulting mixture was stirred for 1 h at the same temperature. Then, 16.7 g (90.0 mmol) of 2-isopropoxy-4,4,5,5-tetramethyl-1,3,2-dioxaborolane was added. After that the cooling bath was removed, and the resulting mixture was stirred for 1 h at room temperature. Finally, 10 mL of water was added, and the obtained mixture was evaporated to dryness. The residue was diluted with 200 mL of water, and crude product was extracted with 3×100 mL of ethyl acetate. The combined organic extract was dried over Na₂SO₄and then evaporated to dryness. Yield 15.0 g (98%) of a yellow oil. Anal. Calc. for C₂₂H₂₈BNO₂: C, 75.65; H, 8.08; N, 4.01. Found: C, 75.99; H, 8.32; N, 3.79. ¹H NMR (CDCl₃): δ 7.59 (m, 1H), 7.18-7.23 (m, 4H), 6.71-6.74 (m, 3H), 5.25 (m, 1H), 3.87 (br.s, 1H, NH), 2.76-2.90 (m, 2H), 2.12-2.16 (m, 1H), 1.75-1.92 (m, 3H), 1.16 (s, 6H), 1.10 (s, 6H).

2-(8-Anilino-5,6,7,8-tetrahydronaphthalen-1-yl)-N-(2,6-diisopropylphenyl)quinolin-8-amine

To a solution of 13.8 g (41.0 mmol) of 2-chloro-N-(2,6-diisopropylphenyl)quinolin-8-amine in 700 mL of 1,4-dioxane were added 15.0 g (43.0 mmol) of N-phenyl-8-(4,4,5,5-tetramethyl-1,3,2-dioxaborolan-2-yl)-1,2,3,4-tetrahydronaphthalen-1-amine, 35.0 g (107 mmol) of cesium carbonate and 400 mL of water. The obtained mixture was purged with argon for 10 min followed by an addition of 2.48 g (2.15 mmol) of Pd(PPh₃)₄. The formed mixture was stirred for 2 h at 90° C., then cooled to room temperature. To the obtained two-phase mixture 700 mL of n-hexane was added. The organic layer was separated, washed with brine, dried over Na₂SO₄, and then evaporated to dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um, eluent: hexane-ethyl acetate-triethylamine=100:5:1, vol.) and then re-crystallized from 150 mL of n-hexane. Yield 15.1 g (70%) of a yellow powder. Anal. calc. for C₃₇H₃₉N₃: C, 84.53; H, 7.48; N, 7.99. Found: C, 84.60; H, 7.56; N, 7.84. ¹H NMR (CDCl₃): δ 7.85-7.87 (d, J=7.98 Hz, 1H), 7.56 (br.s, 1H), 7.43-7.45 (d, J=8.43 Hz, 1H), 7.21-7.38 (m, 6H), 7.12 (t, J=7.77 Hz, 1H), 6.87-6.89 (d, J=7.99 Hz, 1H), 6.74 (t, J=7.99 Hz, 1H), 6.36 (t, J=7.32 Hz, 1H), 6.14-6.21 (m, 3H), 5.35 (br.s, 1H), 3.56 (br.s, 1H), 3.20-3.41 (m, 2H), 2.83-2.99 (m, 2H), 2.10-2.13 (m, 1H), 1.77-1.92 (m, 3H), 1.13-1.32 (m, 12H).

Complex 2 (2-(8-anilino-5,6,7,8-tetrahydronaphthalen-1-yl)-N-(2,6-diisopropylphenyl) quinolin-8-amido hafnium dimethyl)

Benzene (50 mL) was added to 2-(8-Anilino-5,6,7,8-tetrahydronaphthalen-1-yl)-N-(2,6-diisopropylphenyl)quinolin-8-amine (2.21 g, 4.20 mmol) and Hf(NMe₂)₄(1.58 g, 4.45 mmol) to form a clear orange solution. The mixture was heated to reflux for 16 hours to form a clear red-orange solution. Most of the volatiles were removed by evaporation under a stream of nitrogen to afford a concentrated red solution (ca. 5 mL) that was warmed to 40° C. Then hexane (30 mL) was added and the mixture was stirred to cause orange crystalline solid to form. This slurry was cooled to −40° C. for 30 minutes then the solid was collected by filtration and washed with additional cold hexane (2×10 mL). The resulting quinolinyldiamide hafnium diamide was isolated as an orange solid and dried under reduced pressure (2.90 g, 3.67 mmol, 87.4% yield). This solid was dissolved in toluene (25 mL) and Me₃Al (12.8 mL, 25.6 mmol) was added. The mixture was warmed to 40° C. for 1 hour then evaporated under a stream of nitrogen. The crude product (2.54 g) was ˜90% pure by ¹H NMR spectroscopy. The solid was purified by recrystallization from CH₂Cl₂-hexanes (20 mL-20 mL) by slow evaporation to give pure product as orange crystals (1.33 g, 43.2% from ligand). The mother liquor was further concentrated for a second crop (0.291 g, 9.5% from ligand).

Polymerization

For the data reported in Table 1, polymerizations were carried out in a continuous stirred tank reactor system. A 1-liter Autoclave reactor was equipped with a stirrer, a pressure controller, and a water cooling/steam heating element with a temperature controller. The reactor was operated in liquid fill condition at a reactor pressure in excess of the bubbling point pressure of the reactant mixture, keeping the reactants in liquid phase. Isohexane and propylene were pumped into the reactors by Pulsa feed pumps. All flow rates of solvent and liquid monomers were controlled using Coriolis mass flow controller (Quantim series from Brooks). Ethylene flowed as a gas under its own pressure through a Brooks flow controller. Ethylene and propylene feeds were combined into one stream and then mixed with a pre-chilled isohexane stream that had been cooled to at least 0° C. The mixture was then fed to the reactor through a single line. Solutions of tri-n-octyl aluminum (TNOA) or AVTA was added to the combined solvent and monomer stream just before they entered the reactor. Catalyst solution was fed to the reactor using an ISCO syringe pump through a separated line.

Isohexane (used as solvent), and monomers (e.g., ethylene and propylene) were purified over beds of alumina and molecular sieves. Toluene for preparing catalyst solutions was purified by the same technique.

The 100 mg of Complex 1 was activated with N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate at a molar ratio of about 1:1 in 900 ml of toluene to form an active catalyst solution. The solution of tri-n-octyl aluminum (25 wt % in hexane, Sigma Aldrich) was further diluted in isohexane at a concentration of 2.75×10⁻⁶mol/liter. AVTA was diluted in toluene at the concentration of 3.98×10⁻⁵mol/liter.

The polymer produced in the reactor exited through a back pressure control valve that reduced the pressure to atmospheric. This caused the unconverted monomers in the solution to flash into a vapor phase which was vented from the top of a vapor liquid separator. The liquid phase, comprising mainly polymer and solvent, was collected for polymer recovery. The collected samples were first air-dried in a hood to evaporate most of the solvent, and then dried in a vacuum oven at a temperature of about 90° C. for about 12 hours. The vacuum oven dried samples were weighed to obtain yields.

The detailed polymerization process conditions and some characteristic properties are listed in Table 1. The catalyst feed rates may also be adjusted according to the level of impurities in the system to reach the targeted conversions listed. All the reactions were carried out at a pressure of about 2.4 MPa/g unless otherwise mentioned. For comparison, TNOA solution was used in Examples C1 and C2 instead of AVTA. AVTA1 and AVTA2 were prepared as described in Examples 1 and 2, respectively.

TABLE 1

Ethylene-propylene co-polymerization runs using AVTA1, AVTA2 or TNOA

Example #
C1
EP-1
EP-2
C2
EP-3
EP-4
EP-5

Polymerization
120
120
120
120
120
120
120

temperature (° C.)

Ethylene feed rate
4.52
4.52
4.52
4.52
4.52
4.52
4.52

(g/min)

Propylene feed
6
6
6
6
6
6
6

rate (g/min)

Isohexane feed
55.2
55.2
55.2
56.7
54
54
54

rate (g/min)

Catalyst feed rate
2.3 × 10⁻⁷
2.3 × 10⁻⁷
2.3 × 10⁻⁷
2.3 × 10⁻⁷
2.3 × 10⁻⁷
2.3 × 10⁻⁷
3.1 × 10⁻⁷

(mol/min)

Scavenger
TNOA
AVTA1
AVTA 1
TNOA
AVTA2
AVTA2
AVTA2

Scavenger rate
7.4 × 10⁻⁰⁶
8 × 10⁻⁵
0.00012
7.4 × 10⁻⁰⁶
6 × 10⁻⁵
0.00012
0.00012

(mol/min)

Conversion (%)
75.2%
67.1%
56.2%
76.0%
65.6%
57.3%
69.2%

MFR (@230° C.
0.44
1.48
2.65
0.172
0.976
5.77
13.48

g/10 min)

ML (mu)
57.7
24
15.3
77
23.4
10.7
7.7

MLRA (mu-sec)
73.7
30.7
15.5
181.3
102.8
41.9
19

Mn_DRI (g/mol)
96,978
56,898
39,944
106,773
50,055
28,151
27,932

Mw_DRI (g/mol)
245,849
138,759
119,214
278,111
130,268
80,034
77,570

Mz_DRI (g/mol)
547,111
250,185
230,664
524,924
280,281
192,962
180,749

MWD
2.54
2.44
2.98
2.6
2.6
2.84
2.78

Mn_LS (g/mol)
110,311
68,550
54,693
124,715
56,912
35,202
33,107

Mw_LS (g/mol)
208,406
131,615
119,455
266,390
123,924
80,987
76,407

Mz_LS (g/mol)
308,565
227,558
255,769
447,346
236,411
200,636
174,741

g′_vis
0.961
0.95
0.933
1.016
0.92
0.907
0.89

Ethylene (wt %)
55.04
59.45
64.9
55.4
60.02
65.79
60.76

Vinyls/1000 C
0.03
0.05
0.07

vinyl %
21.4
31.2
53.8

For data reported in Tables 2 to 5, all examples were produced using a solution process in a 1.0-liter continuous stirred-tank reactor (autoclave reactor). The autoclave reactor was equipped with a stirrer, a water-cooling/steam-heating element with a temperature controller, and a pressure controller. Solvents and monomers were purified by passing through purification columns packed with molecular sieves. Isohexane (solvent) was passed through four columns in series whereas ethylene, propylene, and toluene were each purified by passing through two columns in series. Purification columns are regenerated periodically (˜twice/year) or whenever there is evidence of low catalyst activity. ENB was purified in a glove box by passing through a bed of basic alumina under a steady nitrogen gas purge. Aluminum Vinyl Transfer Agent (AVTA) solution was diluted to a concentration of 3.38×10⁻⁶mol/ml using isohexane.

Isohexane and AVTA solutions were fed using Pulsa pumps and their flow rate was controlled using a pump calibration curve. Purified propylene, and ENB were also fed using Pulsa pumps but their flow rate was controlled using mass-flow controllers. The feed rate of purified ethylene was also regulated using a mass flow controller. Ethylene and propylene combined into a single line before entering a manifold upstream of the reactor. Isohexane, AVTA solution, and ethylene norbornene (ENB) solution lines also combined in a single line before entering the same manifold. The resulting two lines merged further downstream and the combined mixture of monomers and solvent was fed into the reactor using a single tube.

Catalyst used in Tables 2 to 4 was Complex 1 activated by N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate. Catalyst used in Tables 5 to 6 was Complex 2 activated by N, N-dimethyl-anilinium-tetrakis(pentafluorophenyl) borate. Catalyst solution was prepared daily and used on the same day. The solution was prepared by dissolving 80 mg of Complex 1 or 2 and 90.7 mg of N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate in 900 ml toluene (catalyst concentration=1.233×10⁻⁰⁷mol/ml, pre-catalyst/activator (molar ratio)=0.98). This solution was pumped into the reactor through a designated dip-tube at a desired rate using an Isco pump.

Composition was controlled by adjusting the feed ratio of the monomers. Two studies were made with both EP and EPDM polymers. In the first study (Table 2), the effect of AVTA feed rate on polymer molecular weight was examined by keeping all other feed rates constant and observing the effect of AVTA feed-rate on polymer MFR (or ML). In the second study (Table 3), the effect of reactor residence time on the molecular weight of polymer was examined by holding all monomer and AVTA feed rates constant and observing the effect of isohexane (diluent) flow-rate on polymer MFR (or ML). In the third study (Table 5), both the catalyst and AVTA were changed to complex 2 and AVTA4, respectively, with an emphasis on studying the residence time on branching development in EPDM polymers.

Irganox 1076 was added to the polymer samples as they were collected from the reactor. The polymer samples were then placed on a boiling-water steam table in a hood to evaporate a large fraction of the solvent and unreacted monomers, and then, dried in a vacuum oven at a temperature of about 90° C. for about 12 hours. The vacuum oven dried samples were weighed to obtain yields. The ethylene and ENB content of the polymer was determined by FTIR. The monomer conversions were calculated using the polymer yield, composition and the amount of monomers fed into the reactor. Catalyst activity (also referred as to catalyst productivity) was calculated based the yield and the feed rate of catalyst. All the reactions were carried out at a gauge pressure of about 2.2 MPa. Melt flow rate (MFR) measurements were made as a proxy for molecular weight for the EP copolymers whereas; Mooney measurements were made to gauge the molecular weight and long-chain branching of the EPDM terpolymers.

TABLE 2

Ethylene-propylene co-polymerization runs using AVTA3

Example #
EP-6
EP-7
EP-8
EP-9
EP-10
EP-11

Reactor Temp (° C.)
85
85
85
85
85
85

Reactor Pressure
320
320
320
320
320
320

(psig)

Ethylene Feed
0.8
0.8
0.8
0.8
0.8
0.8

(g/min)

Propylene Feed
14
14
14
14
14
14

(g/min)

Catalyst Feed
1.356 × 10⁻⁶
1.356 × 10⁻⁶
1.356 × 10⁻⁶
1.356 × 10⁻⁶
1.356 × 10⁻⁶
1.356 × 10⁻⁶

(mol/min)

Activator Feed
1.384 × 10⁻⁶
1.384 × 10⁻⁶
1.384 × 10⁻⁶
1.384 × 10⁻⁶
1.384 × 10⁻⁶
1.384 × 10⁻⁶

(mol/min)

AVTA3 feed
3.38 × 10⁻⁵
2.03 × 10⁻⁵
1.35 × 10⁻⁵
3.38 × 10⁻⁵
3.38 × 10⁻⁵
3.38 × 10⁻⁵

(mol/min)

Isohexane feed
64.7
62.1
60.8
65.3
45
23.9

(g/min)

Yield (g/min)
2.7
3.6
3.8
3.3
4.4
3.9

Catalyst efficiency
27102
36614
38557
34057
45000
39886

(g polymer/g cat)

C2 (wt %) -FTIR
21.4
16.6
12.9
17.9
13.2
12.5

MFR (@230° C.,
16.74
1.9
0.65
15
6.67
2.92

g/10 min)

TABLE 3

Ethylene-propylene-ethylidenenorbornene co-polymerization runs using AVTA3

Example #
EPDM-1
EPDM-2
EPDM-3
EPDM-4
EPDM-5
EPDM-6

Reactor Temp (° C.)
100
100
100
100
100
100

Reactor Pressure
320
320
320
320
320
320

(psig)

Ethylene Feed
1.8
1.8
1.8
2.2
2.2
2.2

(g/min)

Propylene Feed
7
7
7
7
7
7

(g/min)

ENB Feed (g/min)
0.4
0.4
0.4
0.49
0.49
0.49

Catalyst Feed
2.446 × 10⁻⁶
2.446 × 10⁻⁶
2.446 × 10⁻⁶
2.446 × 10⁻⁶
2.446 × 10⁻⁶
2.446 × 10⁻⁶

(mol/min)

Activator Feed
2.516 × 10⁻⁶
2.516 × 10⁻⁶
2.516 × 10⁻⁶
2.516 × 10⁻⁶
2.516 × 10⁻⁶
2.516 × 10⁻⁶

(mol/min)

AVTA feed
3.38 × 10⁻⁵
2.03 × 10⁻⁵
1.35 × 10⁻⁵
3.38 × 10⁻⁵
3.38 × 10⁻⁵
3.38 × 10⁻⁵

(mol/min)

Isohexane feed
64.7
62.1
60.8
65.3
45
23.9

(g/min)

Yield (g/min)
2.2
2.3
2.3
1.9
2.5
3.8

Catalyst efficiency
12113
13144
12825
10418
14108
21600

(g polymer/g cat)

C2 (wt %)
56.2
52.8
53.4
59.2
52.3
58.4

uncorrected-FTIR

ENB (wt %)- FTIR
4.9
4.9
4.9
5.3
5.5
5.4

Irganox 1076
208
1065
1129
772
666
233

(ppm)-FTIR

ML(mu)
17.6
42.1
79.8
14
23.8
43.7

MLRA (mu-sec)
50.4
156.5
351.5
38.7
85.8
263.1

cMLRA (mu-sec)
446
394
353
476
492
628

TABLE 4

MW and composition characterization results of ethylene-

propylene-ethylidenenorbornene terpolymers from AVTA3.

Example #
EPDM-1
EPDM-2
EPDM-3
EPDM-4
EPDM-5
EPDM-6

Mn_IR (g/mol)
40,300
60,700
84,900
38,200
46,800
61,900

Mw_IR (g/mol)
101,100
156,600
216,800
94,600
124,200
192,300

Mz_IR (g/mol)
224,400
345,500
437,600
213,000
283,300
500,300

PDI
2.5
2.6
2.55
2.48
2.65
3.10

Mn_LS (g/mol)
42,400
68,100
98,500
39,900
52,000
68,200

Mw_LS (g/mol)
107,000
173,700
240,700
101,100
139,600
213,500

Mz LS (g/mol)
255,000
381,000
484,000
263,700
365,400
632,400

LCB g′_vis
0.951
0.908
0.942
0.949
0.914
0.909

Ethylene (wt %) IR
50.9
47.8
48.8
53.2
45.8
42.5

TABLE 5

Ethylene-propylene-ethylidenenorbornene co-polymerization runs using AVTA4 and catalyst 2 (from complex 2)

Example #
EPDM7
EPDM8
EPDM9
EPDM10
EPDM11
EPDM12
EPDM13
EPDM14

Reactor
100
100
100
100
100
100
100
100

Temp (° C.)

Ethylene
1.8
1.8
2.7
2.7
2.7
2.7
2.7
2.7

Feed

(g/min)

Propylene
7
7
7
7
7
7
7
7

Feed

(g/min)

ENB Feed
0.4
0.4
0.8
0.8
1.11
1.11
1.11
1.11

(g/min)

Catalyst 2
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷

Feed

(mol/min)

AVTA4
2.82 × 10⁻⁵
1.69 × 10⁻⁵
3.38 × 10⁻⁵
2.03 × 10⁻⁵
3.38 × 10⁻⁵
2.03 × 10⁻⁵
3.38 × 10⁻⁵
2.03 × 10⁻⁵

feed

(mol/min)

Isohexane
64.5
61.9
64.8
62.2
65.1
62.4
65.1
62.4

feed

(g/min)

Residence
7.6
7.8
7.4
7.7
7.4
7.6
7.4
7.6

time (min)

Polymer
5.10
5.35
5.54
6.18
4.90
5.06
4.93
4.4

content

(wt %)

Catalyst
14929
12300
16999
16723
11913
15396
12402
10504

efficiency

(g polymer/

g cat)

C2 (wt %)
42.8
42.5
56.0
56.0
57.2
57.3
59.8
61.8

uncorrected-

FTIR

ENB
2.4
2.4
4.4
4.9
6.1
6.1
5.6
5.9

(wt %)-

FTIR

ML (mu)
51.1
77.2
95.8
145.3
92.7
142.6
35.1
56.5

MLRA
202.5
405.4
630.9
1391.1
559.5
1251.1
141.5
265.1

(mu-sec)

cMLRA
386
427
487
589
453
544
463
437

(mu-sec)

Example #
EPDM15
EPDM16
EPDM17
EPDM18
EPDM19
EPDM20
EPDM21
EPDM22

Reactor
100
100
100
100
110
110
110
110

Temp (° C.)

Ethylene
2.6
2.7
2.6
2.6
2.6
2.6
2.6
2.6

Feed

(g/min)

Propylene
7
7
7
7
7
7
7
7

Feed

(g/min)

ENB Feed
1.11
1.11
1.11
1.11
1.11
1.11
1.02
0.93

(g/min)

Catalyst 2
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷
2.47 × 10⁻⁷

Feed

(mol/min)

AVTA4
3.38 × 10⁻⁵
2.03 × 10⁻⁵
2.03 × 10⁻⁵
2.03 × 10⁻⁵
3.69 × 10⁻⁵
3.69 × 10⁻⁵
3.67 × 10⁻⁵
3.67 × 10⁻⁵

feed

(mol/min)

Isohexane
46.3
28.7
43.7
34.7
34.7
28.7
34.6
34.6

feed

(g/min)

Residence
9.6
13.5
10.1
11.9
11.9
13.6
12.0
12.0

time (min)

Polymer
4.90
—
6.94
8.54
10.05
12.61
7.39
6.50

content

(wt %)

Catalyst
9324
16880
15829
16751
16751
18446
15410
12415

efficiency

(g polymer/

g cat)

C2 (wt %)
59.2
57.1
55.8
50.9
56.5
55.3
57.2
57.8

uncorrected-

FTIR

ENB
5.7
6.2
6.2
6.4
6.7
6.5
6.4
5.3

(wt %)-

FTIR

ML (mu)
41
97.4
80
76.6
87.5
90.9
85.3
74.3

MLRA
301.5
1068.9
518.2
561.5
678.1
881.5
651.7
521.2

(mu-sec)

cMLRA
789
805
518
598
596
733
594
580

(mu-sec)

TABLE 6

MW and composition characterization results of ethylene-propylene-

ethylidenenorbornene terpolymers using AVTA4 and catalyst 2

Example #
EPDM7
EPDM8
EPDM9
EPDM10
EPDM11
EPDM12
EPDM13
EPDM14

Mn-IR
69,400
91,200
86,000
109,700
81,200
108,300
49,500
64,000

Mw-IR
187,700
241,600
241,700
310,500
230,600
293,000
141,500
173,400

Mz-IR
430,000
531,600
600,600
753,400
596,600
696,300
445,600
484,600

PDI
2.71
2.65
2.81
2.83
2.84
2.71
2.86
2.71

C2% (IR)
40.93
36.91
53.4
52.6
54.8
55.0
58.0
58.2

LCB g′
0.942
0.938
0.904
0.933
0.914
0.94
0.909
0.891

C2% (NMR)
45.4
44.4
59.2
59.0
60.7
62.5
63.4
65.0

Example #
EPDM15
EPDM16
EPDM17
EPDM18
EPDM19
EPDM20
EPDM21
EPDM22

Mn-IR
50,000
77,900
75,700
72,200
78,600
79,300
75,100
68,200

Mw-IR
153,000
288,000
229,000
233,500
267,800
290,800
243,400
214,600

Mz-IR
568,400
911,300
617,800
674,600
783,200
889,500
698,000
652,700

PDI
3.06
3.70
3.03
3.23
3.41
3.67
3.24
3.15

C2% (IR)
61.1
56.4
52.5
51.8
52.0
50.9
52.9
58.85

LCB g′
0.874
0.85
0.917
0.895
0.878
0.856
0.907
0.897

C2% (NMR)
67.9
63.4
—
60.1
60.7
60.0
60.3
63.0

Molecular weight and composition characterization results of all EPDMs synthesized are tabulated in Tables 4 and 6. Compositions, molecular weights, Mooney and Mooney relaxation values of comparative EPDMA and EPDMB, grades typically useful for foaming applications, are listed in Table 7. Foaming applications demand polymer products to have high melt strength, melt extensibility, and extensional flow hardening which, in turn, require the polymer products to have branch-on-branch long chain branched (LCB) structures. Discussions and characterization of these branch-on-branch structures in foaming grade EPDMs can be found in Rubber Chemistry and Technology, Vol. 86, No. 4, pp. 503-520 (2013). Conventional EPDMs, such as EPDMA and EPDMB, are made with the Ziegler Natta vanadium catalyst and are more linear after polymerization. For them to have branch-on-branch structures, a post-polymerization acid-catalyzed partial crosslinking was introduced to create these LCB structures. One of the consequences of the post-polymerization crosslinking is the gel side-products that need removal during the polymer product finishing. By comparing Tables 5 to 7, it is shown that EPDM16 and EPDM20 are quite comparable with EPDMA and EPDMB. Their rheological responses will be discussed next and show that they have similar branch-on-branch structures as those presence in EPDMA and EPDMB. A residence time of greater than 12 minutes is required in a CSTR solution reactor to promote the development of these branch-on-branch structures.

TABLE 7

MW and composition characterization results of commercial EPDMs

with known branch-on-branch structures for foaming processing.

Control
EPDMA
EPDMB

Mn_IR (g/mol)
71,100
74,700

Mw_IR (g/mol)
266,900
281,900

Mz_IR (g/mol)
817,600
929,600

PDI (Mw/Mn)
3.75
3.77

Ethylene (wt %) IR
49.88
49.07

LCB g′_vis
0.773
0.727

ML (mu)
91
90

MLRA
790
760

cMLRA
656
641

C2 (%)
53
53

ENB (%)
5.7
8.9

Polymer Rheology—Large Angle Oscillatory Shear and Small Angle Oscillatory Shear

Large Amplitude Oscillatory Shear (LAOS) can provide useful characterization in the non-linear viscoelastic spectrum of polymers. LAOS can be described as the oscillatory strain domain where the shear complex modulus (G*) is not merely a function of angular frequency (ω), but also a function of both ω & and strain, (γ). LAOS's tests were conducted using the ATD®1000 rubber process analyzer by Alpha Technologies. The ATD® 1000 is a dynamic mechanical rheological tester designed for testing unfilled elastomers and compounds. Rheological tests using large amplitude oscillatory shear were carried out at a temperature of 125° C., strain of 1000% and frequency of 0.63 rad/sec. The input strain is represented by the function

γ=γ₀sin ωt

where γ₀is the strain amplitude. The stress response of the polymer sample can be represented as a Fourier series

$σ (t; ω; γ_{0}) = γ_{0} \sum_{n} {G^{'} (ω, γ_{0}) \sin n ω t + G^{″} (ω, γ_{0}) \cos n ω t}$

in which G′ and G″ correspond to the real and imaginary component of the complex modulus, G*. The long-chain branching (LCB) index is calculated using the expressions (Burhin et. al., XVth International Congress on Rheology, Monterey, Calif., and August, 2008)

$LCB index = G_{1}^{'} / G_{5}^{'} - E_{3}$

$E_{3} = \frac{5}{4} + \frac{1}{4} {(\frac{G_{3}^{'}}{G_{5}^{'}})}^{2} - \frac{1}{2} \frac{G_{3}^{'}}{G_{5}^{'}}$

where, G′₁, G′₃and G′₅are the first, third and fifth harmonic associated with the real component G′ of the complex modulus (G*). A higher LCB index value is normally associated with increased branching level in the polymer.

Small Angle Oscillatory Shear (SAOS) measurements were carried out using the ATD® 1000 Rubber Process Analyzer from Alpha Technologies. A sample of approximately 4.5 gm weight is mounted between the parallel plates of the ATD® 1000. The test temperature is either 100° C. or 125° C., the applied strain is 14% and the frequency was varied from 0.1 rad/s to 200 rad/s. The complex modulus (G*), complex viscosity (η*) and the phase angle (δ) are measured at each frequency. The phase angle δ, is the inverse tangent of the ratio of G″ (shear loss modulus) to G′ (shear storage modulus). For a typical linear polymer, the phase angle approaches 90° at low frequencies (or long times), since the polymer chains can relax quickly in the melt, absorbing energy and making G″ much larger than G′. With increasing frequency, the relaxation process is not fast, the polymer chains cannot absorb all the energy imparted in the shear oscillation, with the result the storage modulus G′ increases relative to G″. Eventually at the cross-over point, G′ equals G″ and the phase angle is 45°. At much higher frequencies (or short times), G′ dominates the response over G″, the phase angle approaches 0°, which is indicative of the plateau region. In contrast to linear polymers, branched polymer chains relax very slowly and cannot absorb the energy that is imparted even at very low frequencies, as a result the phase angle never approaches 90° at low frequency. In general, the phase angle at a specified frequency will be much lower for a branched polymer relative to a linear polymer.

Shear-thinning is a rheological response of polymer melts, where the resistance to flow (viscosity) decreases with increasing shear rate. The viscosity is generally constant at low shear rates (Newtonian region) and decreases with increasing shear rate. In the low shear-rate region, the viscosity approaches a terminal value termed the zero shear viscosity, which is often difficult to measure for poly-disperse polymer melts. At the higher shear rate, the polymer chains are oriented in the shear direction, which reduces the number of chain entanglements relative to their un-deformed state. This reduction in chain entanglement results in lower viscosity. A method of quantifying shear-thinning is through the use of the shear-thinning index (STI) defined as

STI=(η_{0.1 rad/s}−η_{128 rad/s})/η_{0.1 rad/s}.

The shear-thinning index increases with branching level and for highly branched polymers, the parameter STI approaches 1, since η_{0.1 rad/s}>>η_{128 rad/s}. Conversely for Newtonian fluids, where the viscosity is independent of shear rate, STI approaches 0. The viscosity data collected over a range of frequency can be modeled using the general form of the Cross Equation (J. M Dealy and K. F Wissbrun, Melt Rheology and Its Role in Plastics Processing Theory and Applications; Van Nostrand Reinhold: New York, p. 162 (1990).

η=η_∞+(η₀−η_∞)/1+(γτ)ⁿ

where η₀is the limiting zero shear viscosity, η_∞ the infinite shear viscosity, τ a relaxation time and n the exponent. The term η_∞ is 0 from the curve fit, with the result the expression reduces to three parameters

η=η₀/1+(γτ)ⁿ.

The relaxation time, τ in the Cross Model can be associated to the poly-dispersity or long-chain branching in the polymer. With increased levels of branching it is expected that τ would be higher compared to a linear polymer of the same molecular weight.

LCB index values, key SAOS parameters, and Cross model fit results for EPDM9 to EPDM22 along with EPDMA and EPDMB are tabulated in Table 8. As shown in FIGS. 2 and 3 and in Table 8, EPDM16 and EPDM20 are quite comparable with EPDMA and EPDMB in their rheological responses indicating the presence of branch-on-branch structures in these EPDMs produced at extended residence time, greater than 13 minutes.

TABLE 8

Rheological characterization results of ethylene-propylene-ethylidenenorbornene

terpolymers using AVTA4 and catalyst 2 and of EPDMA and EPDMB.

SAOS

Cross
Cross

SAOS
(0.245
SAOS
SAOS
Model
Model

LAOS
(0.245
Rad/s)
Shear
VGP
Zero
Relaxation
Cross

LCB
Rad/s)
Viscosity
Thinning
Delta
Shear
Time
Model

Sample
Index
Tan δ
(Pa-s)
Indes
degrees
Viscosity
(sec)
Constant

EPDM7
3.0
1.05
1.6E+05
0.985
42.7
3.89E+05
7.5
0.67

EPDM8
2.9
0.94
2.5E+05
0.990
41.8
6.38E+05
7.8
0.71

EPDM9
3.0
0.80
3.5E+05
0.992
38.7
1.54E+06
20.6
0.71

EPDM10
0.3
0.78
5.2E+05
0.993
37.9
1.89E+06
13.4
0.76

EPDM11
3.0
0.85
3.1E+05
0.990
40.4
9.53E+05
11.0
0.71

EPDM12
0.8
0.82
4.9E+05
0.993
39.8
1.39E+06
8.9
0.77

EPDM13
4.5
1.07
1.1E+05
0.980
43.9
5.19E+05
42.1
0.57

EPDM14
4.2
0.95
1.8E+05
0.986
42.7
6.43E+05
18.2
0.63

EPDM15
6.8
0.98
1.2E+05
0.983
43.5
1.01E+06
125.0
0.57

EPDM16
5.0
0.56
4.2E+05
0.994
29.2
2.81E+07
1339.5
0.71

EPDM17
4.1
0.81
2.9E+05
0.991
38.4
1.62E+06
34.7
0.69

EPDM18
4.7
0.71
3.0E+05
0.992
35.4
2.94E+06
90.8
0.68

EPDM19
4.5
0.69
3.5E+05
0.993
34.6
2.50E+06
46.4
0.71

EPDM20
5.3
0.61
3.7E+05
0.994
31.7
6.47E+06
191.6
0.71

EPDM22
4.9
0.82
2.6E+05
0.990
39.2
1.53E+06
41.9
0.67

EPDMA
8.3
0.60
3.2E+05
0.994
31.4
1.31E+07
728.6
0.70

EPDMB
7.1
0.61
3.17E+05
0.994
32.8
8.44E+06
372.6
0.71

Test Methods

Mooney Large Viscosity (ML) and Mooney Relaxation Area (MLRA):

ML and MLRA are measured using a Mooney viscometer according to ASTM D-1646, modified as detailed in the following description. First, an oven-dried polymer sample for Mooney testing is prepared by being pressed into a flat sheet using a hot press at 150° C. for 3 minutes, to remove any water, solvent, and unreacted monomers from the sample. After 3 minutes, if there are any visible bubbles/voids, the sheet is folded and pressed again between the hot plates of the hot press for an additional 3 minutes. Once the sample is cooled, about 25 g is used for Mooney testing. For Mooney testing, the sample is placed on either side of the rotor. The cavity is filled by pneumatically lowering the upper platen. The upper and lower platens are electrically heated and controlled at 125° C. The torque to turn the rotor at 2 rpm is measured by a torque transducer. Mooney viscometer is operated at an average shear rate of 2 s⁻¹. The sample is pre-heated for 1 minute after the platens are closed. The motor is then started and the torque is recorded for a period of 4 minutes. The results are reported as ML (1+4) 125° C., where M is the Mooney viscosity number, L denotes large rotor, 1 is the pre-heating time in minutes, 4 is the sample run time in minutes after the motor starts, and 125° C. is the test temperature.

The torque limit of the Mooney viscometer is about 100 Mooney units. Mooney viscosity values greater than about 100 Mooney unit cannot generally be measured under these conditions. In this event, a non-standard rotor design is employed with a change in Mooney scale that allows the same instrumentation on the Mooney viscometer to be used for more viscous polymers. This rotor that is both smaller in diameter and thinner than the standard Mooney Large (ML) rotor is termed MST—Mooney Small Thin. Typically when the MST rotor is employed, the test is also run at different time and temperature. The pre-heat time is changed from the standard 1 minute to 5 minutes and the test is run at 200° C. instead of the standard 125° C. Thus, the value will be reported as MST (5+4), 200° C. Note that the run time of 4 minutes at the end of which the Mooney reading is taken remains the same as the standard conditions. According to EP 1 519 967, one MST point is approximately 5 ML points when MST is measured at (5+4@200° C.) and ML is measured at (1+4@ 125° C.). The MST rotor should be prepared as follows:

- 1. The rotor should have a diameter of 30.48+/−0.03 mm and a thickness of 2.8+/−0.03 mm (tops of serrations) and a shaft of 11 mm or less in diameter.
- 2. The rotor should have a serrated face and edge, with square grooves of 0.8 mm width and depth of 0.25-0.38 mm cut on 1.6 mm centers. The serrations will consist of two sets of grooves at right angles to each other (form a square crosshatch).
- 3. The rotor shall be positioned in the center of the die cavity such that the centerline of the rotor disk coincides with the centerline of the die cavity to within a tolerance of +/−0.25 mm. A spacer or a shim may be used to raise the shaft to the midpoint.
- 4. The wear point (cone shaped protuberance located at the center of the top face of the rotor) shall be machined off flat with the face of the rotor.

The MLRA data is obtained from the Mooney viscosity measurement when the rubber relaxes after the rotor is stopped. The MLRA is the integrated area under the Mooney torque-relaxation time curve from 1 to 100 seconds. The MLRA is a measure of chain relaxation in molten polymer and can be regarded as a stored energy term which suggests that, after the removal of an applied strain, the longer or branched polymer chains can store more energy and require longer time to relax. Therefore, the MLRA value of a bimodal rubber (the presence of a discrete polymeric fraction with very high molecular weight and distinct composition) or a long chain branched rubber are larger than a broad or a narrow molecular weight rubber when compared at the same Mooney viscosity values.

Mooney Relaxation Area is dependent on the Mooney viscosity of the polymer, and increases with increasing Mooney viscosity. In order to remove the dependence on polymer Mooney Viscosity, a corrected MLRA (cMLRA) parameter is used, where the MLRA of the polymer is normalized to a reference of 80 Mooney viscosity. The formula for cMLRA is provided below

$cMLRA = {MLRA (\frac{80}{ML})}^{1.44}$

where MLRA and ML are the Mooney Relaxation Area and Mooney viscosity of the polymer sample measured at 125° C. Alternatively, the ratio MLRA/ML may be used to encompass both the MLRA and ML data, in view of MLRA's dependence upon ML. This ratio has the dimension of time. A higher MLRA/ML number signifies a higher degree of melt elasticity for materials with similar value of ML. Long chain branching will slow down the relaxation of the polymer chain, hence increasing the value of MLRA/ML.

Unsaturated Chain Ends:

The number of vinyl chain ends, vinylidene chain ends and vinylene chain ends is determined using ¹H NMR using 1,1,2,2-tetrachloroethane-d₂as the solvent on an at least 400 MHz NMR spectrometer. Proton NMR data is collected at 120° C. in a 5 mm probe using a Varian spectrometer with a ¹H frequency of at least 400 MHz. Data was recorded using a maximum pulse width of 45°, 5 seconds between pulses and signal averaging 120 transients. Spectral signals were integrated and the number of unsaturation types per 1000 carbons was calculated by multiplying the different groups by 1000 and dividing the result by the total number of carbons.

The chain end unsaturations are measured as follows. The vinyl resonances of interest are between from 5.0 to 5.1 ppm (VRA), the vinylidene resonances between from 4.65 to 4.85 ppm (VDRA), the vinylene resonances from 5.31 to 5.55 ppm (VYRA), the trisubstituted unsaturated species from 5.11 to 5.30 ppm (TSRA) and the aliphatic region of interest between from 0 to 2.1 ppm (IA).

The number of vinyl groups/1000 Carbons is determined from the formula: (VRA* 500)/((IA+VRA+VYRA+VDRA)/2)+TSRA). Likewise, the number of vinylidene groups/1000 Carbons is determined from the formula: (VDRA*500)/((IA+VRA+VYRA+VDRA)/2)+TSRA), the number of vinylene groups/1000 Carbons from the formula (VYRA*500)/((IA+VRA+VYRA+VDRA)/2) 25+TSRA) and the number of trisubstituted groups from the formula (TSRA*1000)/((IA+VRA+VYRA+VDRA)/2)+TSRA). VRA, VDRA, VYRA, TSRA and IA are the integrated normalized signal intensities in the chemical shift regions defined above. Vinyl chain ends are reported as a molar percentage of the total number of moles of unsaturated polymer end-groups (that is, the sum of vinyl chain ends, vinylidene chain ends, vinylene chain ends, and trisubstituted olefinic chain ends).

When the polymer contains a diene such as ENB, the calculation of number of vinyl chain ends should be modified. For instance, when a polymer contains ENB, vinyl chain ends are reported as a molar percentage of the total number of moles of the sum of vinyl chain ends, vinylidene chain ends, and vinylene chain ends. That is, trisubstituted olefinic chain ends are excluded when calculating the molar percentage. This is because of the overlap with the exocyclic olefinic region of ENB. Similar types of corrections are required when other dienes are used as monomers, as will be recognized by one of ordinary skill in the art with the benefit of this disclosure. For instance, it is known that when 1,5-octadiene is used a diene monomer, a polymer chain incorporating such dienes would include unreacted unsaturations in the form of vinylenes, so the vinylene groups would need to be excluded in the calculation of number of vinyl groups. Similar exclusions for other diene monomers, when present, will be apparent based upon the unreacted unsaturation type that such other diene monomers bring to the polymer chain. Where no diene monomers are present, the vinyl chain end calculation may include the sum of all of the above types of groups (vinyl, vinylidene, vinylene, and trisubstituted groups).

Molecular Weight:

Molecular weights (number average molecular weight (Mn), weight average molecular weight (Mw), and z-average molecular weight (Mz)) are determined using a Polymer Laboratories Model 220 high temperature GPC-SEC (gel permeation/size exclusion chromatograph) equipped with on-line differential refractive index (DRI), light scattering (LS), and viscometer (VIS) detectors. It uses three Polymer Laboratories PLgel 10 m Mixed-B columns for separation using a flow rate of 0.54 ml/min and a nominal injection volume of 300 microliter. The detectors and columns were contained in an oven maintained at 135° C. The stream emerging from the SEC columns was directed into the miniDAWN optical flow cell and then into the DRI detector. The DRI detector was an integral part of the Polymer Laboratories SEC. The viscometer was inside the SEC oven, positioned after the DRI detector. The details of these detectors as well as their calibrations have been described by, for example, T. Sun et al., in Macromolecules, Volume 34, Number 19, pp. 6812-6820, (2001), incorporated herein by reference.

Solvent for the SEC experiment was prepared by dissolving 6 grams of butylated hydroxy toluene (BHT) as an antioxidant in 4 liters of Aldrich reagent grade 1, 2, 4-trichlorobenzene (TCB). The TCB mixture was then filtered through a 0.7 micrometer glass pre-filter and subsequently through a 0.1 micrometer Teflon filter. The TCB was then degassed with an online degasser before entering the SEC. Polymer solutions were prepared by placing dry polymer in a glass container, adding the desired amount of BHT stabilized TCB, then heating the mixture at 160° C. with continuous agitation for about 2 hours. All quantities were measured gravimetrically. The TCB densities used to express the polymer concentration in mass/volume units are 1.463 g/mL at 22° C. and 1.324 g/mL at 135° C. The injection concentration was from 1.0 to 2.0 mg/mL, with lower concentrations being used for higher molecular weight samples. Prior to running each sample the DRI detector and the injector were purged. Flow rate in the apparatus was then increased to 0.5 mL/minute, and the DRI is allowed to stabilize for 8 to 9 hours before injecting the first sample. The concentration, c, at each point in the chromatogram is calculated from the baseline-subtracted DRI signal, I_DRI, using the following equation:

c=K_DRII_DRI/(dn/dc)

where K_DRIis a constant determined by calibrating the DRI with a series of mono-dispersed polystyrene standards with molecular weight ranging from 600 to 10M, and (dn/dc) is the refractive index increment for the system. The refractive index, n=1.500 for TCB at 145° C. and λ=690 nm. For purposes of this invention and the claims thereto (dn/dc)=0.1048 for ethylene-propylene copolymers, and (dn/dc)=0.01048−0.0016ENB for EPDM, where ENB is the ENB content in wt % in the ethylene-propylene-diene terpolymer. Where other non-conjugated polyenes are used instead of (or in addition to) ENB, the ENB is taken as weight percent of total non-conjugated polyenes. The value (dn/dc) is otherwise taken as 0.1 for other polymers and copolymers. Units of parameters used throughout this description of the SEC method are: concentration is expressed in g/cm³, molecular weight is expressed in g/mol, and intrinsic viscosity is expressed in dL/g.

The light scattering (LS) detector was a high temperature miniDAWN (Wyatt Technology, Inc.). The primary components are an optical flow cell, a 30 mW, 690 nm laser diode light source, and an array of three photodiodes placed at collection angles of 45°, 90°, and 135°. The molecular weight, M, at each point in the chromatogram was determined by analyzing the LS output using the Zimm model for static light scattering (M. B. Huglin, LIGHT SCATTERING FROM POLYMER SOLUTIONS, Academic Press, 1971):

$\frac{K_{o} c}{Δ R (θ)} = \frac{1}{MP (θ)} + 2 A_{2} c .$

Here, ΔR(θ) is the measured excess Rayleigh scattering intensity at scattering angle θ, c is the polymer concentration determined from the DRI analysis, A₂is the second virial coefficient (for purposes of this invention, A₂=0.0015 for ethylene homopolymer and A₂=0.0015−0.00001EE for ethylene-propylene copolymers, where EE is the ethylene content in weight percent in the ethylene-propylene copolymer. P(θ) is the form factor for a mono-disperse random coil, and K_ois the optical constant for the system:

$K_{o} = \frac{4 π^{2} {n^{2} (dn / dc)}^{2}}{λ^{4} N_{A}}$

where N_Ais Avogadro's number, and (dn/dc) is the refractive index increment for the system. The refractive index, n=1.500 for TCB at 145° C. and λ=690 nm. For purposes of this application, where DRI and LS measurements conflict, LS measurements should be used for Mw and Mz, while DRI measurements should be used for Mn.

Branching Index (g′_vis):

A high temperature viscometer from Viscotek Corporation was used to determine specific viscosity. The viscometer has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers. One transducer measures the total pressure drop across the detector, and the other, positioned between the two sides of the bridge, measures a differential pressure. The specific viscosity, η_s, for the solution flowing through the viscometer was calculated from their outputs. The intrinsic viscosity, [η], at each point in the chromatogram was calculated from the following equation:

η_s=c[η]+0.3(c[η])²

where c is concentration and was determined from the DRI output.

The branching index (g′_vis) is defined as the ratio of the intrinsic viscosity of the branched polymer to the intrinsic viscosity of a linear polymer of equal molecular weight and same composition, and was calculated using the output of the SEC-DRI-LS-VIS method as follows. The average intrinsic viscosity, [η]_avg, of the sample was calculated by:

${[η]}_{avg} = \frac{Σ {c_{i} [η]}_{i}}{Σ c_{i}}$

where the summations are over the chromatographic slices, i, between t integration limits.

The branching index g′_visis defined as:

$g_{vis}^{'} = \frac{{[η]}_{avg}}{{kM}_{v}^{α}} .$

The intrinsic viscosity of the linear polymer of equal molecular weight and same composition is calculated using Mark-Houwink equation, where the K and a are determined based on the composition of linear ethylene/propylene copolymer and linear ethylene-propylene-diene terpolymers using a standard calibration procedure. My is the viscosity-average molecular weight based on molecular weights determined by LS analysis. See Macromolecules, 2001, 34, pp. 6812-6820 and Macromolecules, 2005, 38, pp. 7181-7183, regarding selecting a linear standard having similar molecular weight and comonomer content, and determining k coefficients and a exponents.

GPC-4D Procedure: Molecular Weight, Comonomer Composition and Long Chain Branching Determination by GPC-IR Hyphenated with Multiple Detectors:

Unless otherwise indicated, the distribution and the moments of molecular weight (Mw, Mn, Mw/Mn, etc.), the comonomer content (C₂, C₃, C₆, etc.) and the branching index (g′vis) are determined by using a high temperature Gel Permeation Chromatography (Polymer Char GPC-IR) equipped with a multiple-channel band-filter based Infrared detector IR5, an 18-angle light scattering detector and a viscometer. Three Agilent PLgel 10-μm Mixed-B LS columns are used to provide polymer separation. Aldrich reagent grade 1,2,4-trichlorobenzene (TCB) with 300 ppm antioxidant butylated hydroxytoluene (BHT) is used as the mobile phase. The TCB mixture is filtered through a 0.1-μm Teflon filter and degassed with an online degasser before entering the GPC instrument. The nominal flow rate is 1.0 ml/min and the nominal injection volume is 200 μL. The whole system including transfer lines, columns, and detectors are contained in an oven maintained at 145° C. The polymer sample is weighed and sealed in a standard vial with 80-μL flow marker (Heptane) added to it. After loading the vial in the autosampler, polymer is automatically dissolved in the instrument with 8 ml added TCB solvent. The polymer is dissolved at 160° C. with continuous shaking for about 1 hour for most PE samples or 2 hour for PP samples. The TCB densities used in concentration calculation are 1.463 g/ml at room temperature and 1.284 g/ml at 145° C. The sample solution concentration is from 0.2 to 2.0 mg/ml, with lower concentrations being used for higher molecular weight samples. The concentration (c), at each point in the chromatogram is calculated from the baseline-subtracted IR5 broadband signal intensity (I), using the following equation: c=βI, where β is the mass constant. The mass recovery is calculated from the ratio of the integrated area of the concentration chromatography over elution volume and the injection mass which is equal to the pre-determined concentration multiplied by injection loop volume. The conventional molecular weight (IR MW) is determined by combining universal calibration relationship with the column calibration which is performed with a series of monodispersed polystyrene (PS) standards ranging from 700 to 10M g/mole. The MW at each elution volume is calculated with following equation

$\log M = \frac{\log (K_{PS} / K)}{a + 1} + \frac{a_{PS} + 1}{a + 1} \log M_{PS}$

where the variables with subscript “PS” stand for polystyrene while those without a subscript are for the test samples. In this method, α^PS=0.67 and K_PS=0.000175 while a and K are for other materials as calculated as published in literature (Sun, T. et al. Macromolecules, 2001, 34, 6812), except that for purposes of the present disclosure, α=0.700 and K=0.0003931 for ethylene, propylene, diene monomer copolymers (Nota Bene: Example 1 below used K=0.000351 and α=0.701), α=0.695 and K=0.000579 for linear ethylene polymers, α=0.705 and K=0.0002288 for linear propylene polymers, α=0.695 and K=0.000181 for linear butene polymers, α is 0.695 and K is 0.000579*(1−0.0087*w2b+0.000018*(w2b)̂2) for ethylene-butene copolymer where w2b is a bulk weight percent of butene comonomer, α is 0.695 and K is 0.000579*(1−0.0075*w2b) for ethylene-hexene copolymer where w2b is a bulk weight percent of hexene comonomer, and α is 0.695 and K is 0.000579*(1−0.0077*w2b) for ethylene-octene copolymer where w2b is a bulk weight percent of octene comonomer. Concentrations are expressed in g/cm³, molecular weight is expressed in g/mole, and intrinsic viscosity (hence K in the Mark-Houwink equation) is expressed in dL/g unless otherwise noted.

The comonomer composition is determined by the ratio of the IR5 detector intensity corresponding to CH₂and CH₃channel calibrated with a series of PE and PP homo/copolymer standards. In particular, this provides the methyls per 1000 total carbons (CH₃/1000TC) as a function of molecular weight. The short-chain branch (SCB) content per 1000TC (SCB/1000TC) is then computed as a function of molecular weight by applying a chain-end correction to the CH₃/1000TC function, assuming each chain to be linear and terminated by a methyl group at each end. The weight % comonomer is then obtained from the following expression in which f is 0.3, 0.4, 0.6, 0.8, and so on for C₃, C₄, C₆, C₈, and so on comonomers, respectively.

w2=f*SCB/1000TC

The bulk composition of the polymer from the GPC-IR and GPC-4D analyses is obtained by considering the entire signals of the CH₃and CH₂channels between the integration limits of the concentration chromatogram. First, the following ratio is obtained.

$Bulk IR ratio = \frac{Area of {CH}_{3} signal within integration limits}{Area of {CH}_{2} signal within integration limits}$

Then the same calibration of the CH₃and CH₂signal ratio, as mentioned previously in obtaining the CH3/1000TC as a function of molecular weight, is applied to obtain the bulk CH3/1000TC. A bulk methyl chain ends per 1000TC (bulk CH3end/1000TC) is obtained by weight-averaging the chain-end correction over the molecular-weight range. Then

w2b=f*bulk CH3/1000TC

$bulk SCB / 1000 TC = bulk CH 3 / 1000 TC - bulk \frac{CH 3 end}{1000 TC}$

and bulk SCB/1000TC is converted to bulk w2 in the same manner as described above.

The LS detector is the 18-angle Wyatt Technology High Temperature DAWN HELEOSII. The LS molecular weight (M) at each point in the chromatogram is determined by analyzing the LS output using the Zimm model for static light scattering (Light Scattering from Polymer Solutions; Huglin, M. B., Ed.; Academic Press, 1972.).

$\frac{K_{o} c}{Δ R (θ)} = \frac{1}{MP (θ)} + 2 A_{2} c$

Here, ΔR(θ) is the measured excess Rayleigh scattering intensity at scattering angle θ, c is the polymer concentration determined from the IR5 analysis, A₂is the second virial coefficient, P(θ) is the form factor for a monodisperse random coil, and K_ois the optical constant for the system:

$K_{o} = \frac{4 π^{2} {n^{2} (dn / dc)}^{2}}{λ^{4} N_{A}}$

where N_Ais Avogadro's number, and (dn/dc) is the refractive index increment for the system. The refractive index, n=1.500 for TCB at 145° C. and λ=665 nm. For analyzing polyethylene homopolymers, ethylene-hexene copolymers, and ethylene-octene copolymers, dn/dc=0.1048 ml/mg and A₂=0.0015; for analyzing ethylene-butene copolymers, dn/dc=0.1048*(1−0.00126*w2) ml/mg and A₂=0.0015 where w2 is weight percent butene comonomer.

A high temperature Agilent (or Viscotek Corporation) viscometer, which has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers, is used to determine specific viscosity. One transducer measures the total pressure drop across the detector, and the other, positioned between the two sides of the bridge, measures a differential pressure. The specific viscosity, η_S, for the solution flowing through the viscometer is calculated from their outputs. The intrinsic viscosity, [η], at each point in the chromatogram is calculated from the equation [η]=η_S/c, where c is concentration and is determined from the IR5 broadband channel output. The viscosity MW at each point is calculated as

M=K_PSM^α^PS⁺¹/[η],

where α_psis 0.67 and K_PSis 0.000175.

The branching index (g′_vis) is calculated using the output of the GPC-IR5-LS-VIS method as follows. The average intrinsic viscosity, [η]_avg, of the sample is calculated by:

${[η]}_{avg} = \frac{Σ {c_{i} [η]}_{i}}{Σ c_{i}} .$

where the summations are over the chromatographic slices, i, between the integration limits.

The branching index g′_visis defined as

$g_{vis}^{'} = \frac{{[η]}_{avg}}{{KM}_{v}^{α}},$

where M_vis the viscosity-average molecular weight based on molecular weights determined by LS analysis and the K and a are for the reference linear polymer, which are, for purposes of the present disclosure, α=0.700 and K=0.0003931 for ethylene, propylene, diene monomer copolymers, α=0.695 and K=0.000579 for linear ethylene polymers, α=0.705 and K=0.0002288 for linear propylene polymers, α=0.695 and K=0.000181 for linear butene polymers, a is 0.695 and K is 0.000579*(1−0.0087*w2b+0.000018*(w2b)̂2) for ethylene-butene copolymer where w2b is a bulk weight percent of butene comonomer, a is 0.695 and K is 0.000579*(1−0.0075*w2b) for ethylene-hexene copolymer where w2b is a bulk weight percent of hexene comonomer, and a is 0.695 and K is 0.000579*(1−0.0077*w2b) for ethylene-octene copolymer where w2b is a bulk weight percent of octene comonomer. Concentrations are expressed in g/cm³, molecular weight is expressed in g/mole, and intrinsic viscosity (hence K in the Mark-Houwink equation) is expressed in dL/g unless otherwise noted. Calculation of the w2b values is as discussed above.

Experimental and analysis details not described above, including how the detectors are calibrated and how to calculate the composition dependence of Mark-Houwink parameters and the second-virial coefficient, are described by T. Sun, P. Brant, R. R. Chance, and W. W. Graessley (Macromolecules, 2001, Vol. 34(19), pp. 6812-6820).

All molecular weights are weight average unless otherwise noted. All molecular weights are reported in g/mol unless otherwise noted. Methyl groups per 1000 carbons (CH₃/1000Carbons) is determined by ¹H NMR.

Comonomer Content:

(such as for ethylene, butene, hexene, and octene) content is determined using FTIR according the ASTM D3900 and is not corrected for diene content. ENB content is determined using FTIR according to ASTM D6047. The content of other dienes is obtained using C¹³NMR.

13C NMR: The ¹³C solution NMR was performed on a 10 mm broadband probe using a field of at least 400 MHz in tetrachloroethane-d2 solvent at 120° C. with a flip angle of 90° and full NOE with decoupling. Sample preparation (polymer dissolution) was performed at 140° C. where 0.20 grams of polymer was dissolved in an appropriate amount of solvent to give a final polymer solution volume of 3 ml. Chemical shifts were referenced by setting the ethylene backbone (—CH₂—)n (where n>6) signal to 29.98 ppm. Carbon NMR spectroscopy was used to measure the composition of the reactor products as submitted.

Chemical shift assignments for the ethylene-propylene copolymer are described by Randall in ‘A Review Of High Resolution Liquid ¹³Carbon Nuclear Magnetic Resonance Characterization of Ethylene-Based Polymers,’ Polymer Reviews, 29:2, pp. 201-317 (1989). The copolymer content (mole and weight %) is also calculated based on the method established by Randall in this paper. Calculations for r₁r₂were based on the equation r₁r₂=4*[EE]*[PP]/[EP]²; where [EE], [EP], [PP] are the diad molar concentrations; E is ethylene, P is propylene.

The values for the methylene sequence distribution and number average sequence lengths were determined based on the method established by James C. Randall, “Methylene sequence distributions and average sequence lengths in ethylene-propylene copolymers,” Macromolecules, 1978, 11, 33-36.

MFR

The “melt flow rate” (MFR) is measured in accordance with ASTM D 1238 at 230° C. and 2.16 kg load.

Complex viscosity is determined as described in the Experimental section of U.S. Pat. No. 9,458,310. Also see M. Van Gurp, J. Palmen, Rheol. Bull., 1998, 67, 5-8. The dependence of complex viscosity as a function of frequency can also be determined from rheological measurements at 190° C. The following ratio:

[η*(0.1 rad/s)−η*(100 rad/s)]/η*(0.1 rad/s)

was used to measure the degree of shear thinning of the polymeric materials of the embodiments herein, where η*(0.1 rad/s) and η*(100 rad/s) are the complex viscosities at frequencies of 0.1 and 100 rds, respectively, measured at 190° C. The higher this ratio, the higher is the degree of shear thinning.

The transient uniaxial extensional viscosity was measured using a SER-2-A Testing Platform available from Xpansion Instruments LLC, Tallmadge, Ohio, USA. The SER Testing Platform was used on a Rheometrics ARES-LS (RSA3) strain-controlled rotational rheometer available from TA Instruments Inc., New Castle, Del., USA. The SER Testing Platform is described in U.S. Pat. No. 6,578,413 and U.S. Pat. No. 6,691,569, which are incorporated herein for reference. A general description of transient uniaxial extensional viscosity measurements is provided, for example, in “Strain hardening of various polyolefins in uniaxial elongational flow”, The Society of Rheology, Inc., J. Rheol. 47(3), 619-630 (2003) and “Measuring the transient extensional rheology of polyethylene melts using the SER universal testing platform”, The Society of Rheology, Inc., J. Rheol. 49(3), 585-606 (2005), incorporated herein for reference. Strain hardening occurs when a polymer is subjected to uniaxial extension and the transient extensional viscosity increases more than what is predicted from linear viscoelastic theory. Strain hardening is observed as abrupt upswing of the extensional viscosity in the transient extensional viscosity vs. time plot. A strain hardening ratio (SHR) is used to characterize the upswing in extensional viscosity and is defined as the ratio of the maximum transient extensional viscosity over three times the value of the transient zero-shear-rate viscosity at the same strain. Strain hardening is present in the material when the ratio is greater than 1.

All documents described herein are incorporated by reference herein for purposes of all jurisdictions where such practice is allowed, including any priority documents and/or testing procedures to the extent they are not inconsistent with this text. As is apparent from the foregoing general description and the specific embodiments, while forms of the invention have been illustrated and described, various modifications can be made without departing from the spirit and scope of the invention. Accordingly, it is not intended that the invention be limited thereby. Likewise, the term “comprising” is considered synonymous with the term “including.” Likewise whenever a composition, an element or a group of elements is preceded with the transitional phrase “comprising,” it is understood that we also contemplate the same composition or group of elements with transitional phrases “consisting essentially of,” “consisting of,” “selected from the group of consisting of,” or “is” preceding the recitation of the composition, element, or elements and vice versa.