Highly soluble bis-borate as binuclear co-catalysts for olefin polymerization

Abstract

Embodiments are directed to catalyst systems comprising: a procatalyst; and a co-catalyst dissolved in a non-halogenated aprotic hydrocarbon solvent, the co-catalyst comprising: a non-coordinating borate dianion having the formula: (III) and two cations, each cation being independently chosen from a cation according to formula (I) or formula (II).

Description

TECHNICAL FIELD

Embodiments of the present disclosure generally relate to highly soluble binuclear bis-borate co-catalysts.

BACKGROUND

Since the discovery by Ziegler and Natta of heterogeneous olefin polymerizations, global polyolefin production reached approximately 150 million tons per year in 2015, and it is rising due to increasing market demand. This success is based in part on a series of important breakthroughs in co-catalyst technology. The co-catalysts discovered include aluminoxanes, boranes, and borates with triphenylcarbenium or ammonium cations. These co-catalysts activate the homogeneous single-site olefin polymerization procatalysts, and polyolefins have been produced using these co-catalysts in industry.

Borate based co-catalysts in particular have contributed significantly to the fundamental understanding of olefin polymerization mechanisms and have enhanced the ability for precise control over polyolefin microstructures by deliberately tuning catalyst structures and processes. This results in stimulated interest in mechanistic studies and lead to the development of novel homogeneous olefin polymerization catalyst systems that have precise control over polyolefin microstructures and performance.

SUMMARY

Despite the unique properties of the molecular catalyst systems that combine borate co-catalysts and Ziegler-Natta procatalysts, the molecular catalyst systems are not easily solubilized in apolar solvents, such as toluene or methylcyclohexane. Since ethylene and other olefins are often commercially polymerized in apolar solvents, a large amount of solvent or a halogenated solvent, such as difluorobenzene, dichlorobenzene, dichloromethane, and chloroform, is used to dissolve the components of the catalyst system. However, trace amounts of halogenated solvents may interact adversely with the co-catalysts, and a small amount of halogenated solvent may greatly decrease the activity of the catalyst system, which may affect the polymer yield and other polymer properties. Additionally, if the procatalyst or co-catalyst is insoluble or slightly soluble in the solvent, the activity of the catalyst system could be greatly decreased as well. As a result, there is an ongoing need to solubilize a catalyst system in a small amount of solvent, preferably in an apolar solvent, while maintaining catalyst efficiency, reactivity, and the ability to produce polymers with good physical properties.

According to some embodiments, a catalyst system may include a procatalyst; and a co-catalyst having a non-coordinating borate dianion having the formula:

and two cations according to formula (I) or formula (II):

In formula (I), each R¹, R², R³, R⁴, and R⁵ is independently chosen from —H, —F, —Cl, substituted (C₄-C₄₀)alkyl, unsubstituted (C₄-C₄₀)alkyl, substituted (C₄-C₄₀)cycloalkyl, or unsubstituted (C₄-C₄₀)cycloalkyl. The substituted (C₄-C₄₀)cycloalkyl and substituted (C₄-C₄)alkyl are substituted with one or more than one R^S, where each R^S is chosen from (C₁-C₂₀)alkyl or halogen. Moreover, at least one of R¹, R², R³, R⁴, or R⁵ is chosen from (C₄-C₄₀) alkyl; and in formula (II), each R⁶ and R⁷ is chosen from (C₄-C₃₀)alkyl, and R⁸ is chosen from (C₁-C₂₀)alkyl or (C₆-C₁₈)aryl. The cocatalyst may be dissolved in a non-halogenated hydrocarbon solvent.

BRIEF DESCRIPTION OF FIGURES

FIG. 1 is an illustration of the crystal structure of the Inventive Co-Catalyst 2 as disclosed. Thermal ellipsoids are drawn at the 30% probability level. H atoms are omitted for clarity.

FIG. 2 is a stacked variable temperature (VT) fluorine (¹⁹F) nuclear magnetic resonance (NMR) spectroscopy of Inventive Co-Catalyst 2 in C₆D₅Cl at four different temperatures: 10° C., 60° C., 80° C., and 120° C. Only —C₆F₄— region of the VT-¹⁹F NMR spectrum of Inventive Co-Catalyst 2 is shown.

DETAILED DESCRIPTION

Specific embodiments of catalyst systems will now be described. It should be understood that the catalyst systems of this disclosure may be embodied in different forms and should not be construed as limited to the specific embodiments set forth in this disclosure. Rather, embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the subject matter to those skilled in the art.

Common abbreviations are listed below:

Me: methyl; Et: ethyl; Ph: phenyl; Bn: benzyl; i-Pr: iso-propyl; t-Bu: tert-butyl; t-Oct: tert-octyl (2,4,4-trimethylpentan-2-yl); Tf: trifluoromethane sulfonate; THF: tetrahydrofuran; Et₂O: diethyl ether; CH₂Cl₂: dichloromethane; CV: column volume (used in column chromatography); EtOAc: ethyl acetate; C₆D₆: deuterated benzene or benzene-d6 CDCl₃: deuterated chloroform; Na₂SO₄: sodium sulfate; MgSO₄: magnesium sulfate; HCl hydrogen chloride; n-BuLi: butyllithium; t-BuLi: tert-butyllithium; N₂: nitrogen gas; PhMe: toluene; T: toluene MAO: methylaluminoxane; MMAO: modified methylaluminoxane; GC: gas chromatography; LC: liquid chromatography; NMR: nuclear magnetic resonance; MS: mass spectrometry; mmol: millimoles; mL: milliliters; M: molar; min or mins: minutes; h or hrs: hours; d: day or days.

The term “independently selected” is used herein to indicate that the R groups, such as, R¹, R², R³, R⁴, and R⁵, can be identical or different (e.g., R¹, R², R³, R⁴, and R⁵ may all be substituted alkyls or R¹ and R² may be a substituted alkyl and R³ may be an aryl, etc.). A chemical name associated with an R group is intended to convey the chemical structure that is recognized in the art as corresponding to that of the chemical name. Thus, chemical names are intended to supplement and illustrate, not preclude, the structural definitions known to those of skill in the art.

The term “procatalyst” refers to a transition metal compound that has olefin polymerization catalytic activity when combined with an activator. The term “activator” refers to a compound that chemically reacts with a procatalyst in a manner that converts the procatalyst to a catalytically active catalyst. As used herein, the terms “co-catalyst” and “activator” are interchangeable terms.

When used to describe certain carbon atom-containing chemical groups, a parenthetical expression having the form “(C_x-C_y)” means that the unsubstituted form of the chemical group has from x carbon atoms to y carbon atoms, inclusive of x and y. For example, a (C₁-C₅₀)alkyl is an alkyl group having from 1 to 50 carbon atoms in its unsubstituted form. In some embodiments and general structures, certain chemical groups may be substituted by one or more substituents such as R^S. An R^S substituted chemical group defined using the “(C_x-C_y)” parenthetical may contain more than y carbon atoms depending on the identity of any groups R^S. For example, a “(C₁-C₅₀)alkyl substituted with exactly one group R^S, where R^S is phenyl (—C₆H₅)” may contain from 7 to 56 carbon atoms. Thus, in general when a chemical group defined using the “(C_x-C_y)” parenthetical is substituted by one or more carbon atom-containing substituents R^S, the minimum and maximum total number of carbon atoms of the chemical group is determined by adding to both x and y the combined sum of the number of carbon atoms from all of the carbon atom-containing substituents R^S.

The term “substitution” means that at least one hydrogen atom (—H) bonded to a carbon atom or heteroatom of a corresponding unsubstituted compound or functional group is replaced by a substituent (e.g., R^S). The term “—H” means a hydrogen or hydrogen radical that is covalently bonded to another atom. “Hydrogen” and “—H” are interchangeable, and unless clearly specified have identical meanings.

The term “(C₁-C₅₀)alkyl” means a saturated straight or branched hydrocarbon radical of from 1 to 50 carbon atoms; and the term “(C₁-C₃₀)alkyl” means a saturated straight or branched hydrocarbon radical of from 1 to 30 carbon atoms. Each (C₁-C₅₀)alkyl and (C₁-C₃)alkyl may be unsubstituted or substituted by one or more R^S. In some examples, each hydrogen atom in a hydrocarbon radical may be substituted with R^S, such as, for example trifluoromethyl. Examples of unsubstituted (C₁-C₅₀)alkyl are unsubstituted (C₁-C₂₀)alkyl; unsubstituted (C₁-C₁₀)alkyl; unsubstituted (C₁-C₅)alkyl; methyl; ethyl; 1-propyl; 2-propyl; 1-butyl; 2-butyl; 2-methylpropyl; 1,1-dimethylethyl; 1-pentyl; 1-hexyl; 1-heptyl; 1-nonyl; and 1-decyl. Examples of substituted (C₁-C₄₀)alkyl are substituted (C₁-C₂₀)alkyl, substituted (C₁-C₁₀)alkyl, trifluoromethyl, and [C₄₅]alkyl. The term “[C₄₅]alkyl” means there is a maximum of 45 carbon atoms in the radical, including substituents, and is, for example, a (C₇-C₀)alkyl substituted by one R^S, which is a (C₁-C₅)alkyl, respectively. More broadly, the term “[C_z]alkyl” means there is a maximum of z carbon atoms, wherein z is a positive integer, in the radical, including substituents. Each (C₁-C₅)alkyl may be methyl, trifluoromethyl, ethyl, 1-propyl, 1-methylethyl, or 1,1-dimethylethyl.

The term (C₃-C₅)alkenyl means a branched or unbranched, cyclic or acyclic monovalent hydrocarbon radical containing 3 to 50 carbon atoms, at least one double bond and is unsubstituted or substituted by one or more R^S. Examples of unsubstituted (C₃-C₅₀)alkenyl: n-propenyl, isopropenyl, n-butenyl, isobutenyl, octenyl, decenyl, cyclopentenyl, cyclopentadienyl, cyclohexenyl, and cyclohexadienyl. Examples of substituted (C₃-C₅₀)alkenyl: (2-trifluoromethyl)pent-1-enyl, (3-methyl)hex-1-eneyl, (3-methyl)hexa-1,4-dienyl and (Z)-1-(6-methylhept-3-en-1-yl)cyclohex-1-eneyl.

The term “(C₃-C₅₀)cycloalkyl” means a saturated cyclic monovalent hydrocarbon radical of from 3 to 50 carbon atoms that is unsubstituted or substituted by one or more R^S. Other cycloalkyl groups (e.g., (C_x—C_y)cycloalkyl) are defined in an analogous manner as having from x to y carbon atoms and being either unsubstituted or substituted with one or more R^S Examples of unsubstituted (C₃-C₄₀)cycloalkyl are unsubstituted (C₃-C₂₀)cycloalkyl, unsubstituted (C₃-C₁₀)cycloalkyl, cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cycloheptyl, cyclooctyl, cyclononyl, and cyclodecyl. Examples of substituted (C₃-C₄₀)cycloalkyl are substituted (C₃-C₂₀)cycloalkyl, substituted (C₃-C₁₀)cycloalkyl, and 1-fluorocyclohexyl.

The term “halogen atom” or “halogen” means the radical of a fluorine atom (F), chlorine atom (C), bromine atom (Br), or iodine atom (I). The term “halide” means anionic form of the halogen atom, e.g., fluoride (F⁻), chloride (Cl⁻), bromide (Br⁻), or iodide (I⁻).

The term “saturated” means lacking carbon-carbon double bonds, carbon-carbon triple bonds, and (in heteroatom-containing groups) carbon-nitrogen, carbon-phosphorus, and carbon-silicon double bonds. Where a saturated chemical group is substituted by one or more substituents R^S, one or more double or triple bonds optionally may be present in substituents R^S. The term “unsaturated” means containing one or more carbon-carbon double bonds or carbon-carbon triple bonds, or (in heteroatom-containing groups) one or more carbon-nitrogen double bonds, carbon-phosphorus double bonds, or carbon-silicon double bonds, not including double bonds that may be present in substituents R^S, if any, or in aromatic rings or heteroaromatic rings, if any.

Embodiments of this disclosure include catalyst systems that include a catalyst; and a co-catalyst comprising: a non-coordinating dianionic borate compound having the formula:

and two cations according to formula (I) or formula (II):

In formula (I), each R¹, R², R³, R⁴, and R⁵ is independently chosen from —H, —F, —Cl, substituted or unsubstituted (C₄-C₄)alkyl, substituted or unsubstituted (C₄-C₄)alkenyl or substituted or unsubstituted (C₄-C₄₀)cycloalkyl. The substituted (C₄-C₄₀)alkyl and substituted (C₄-C₄₀)cycloalkyl are substituted with one or more R^S, where each R^S is chosen from (C₁-C₂₀)alkyl, —F and —Cl. Moreover, at least one of R¹, R², R³, R⁴, or R⁵ is chosen from (C₄-C₄₀) alkyl.

In formula (II), each R⁶ and R⁷ is chosen from (C₄-C₃₀)alkyl, and R⁸ is chosen from (C₁-C₂₀)alkyl or (C₆-C₁₈)aryl. The co-catalyst may be dissolved in a non-halogenated aprotic hydrocarbon solvent. In some embodiments, the co-catalyst may be dissolved in an alkane solvent.

In some embodiments of formula (I), each R¹, R², R³, R⁴, and R⁵ is independently chosen from —H, (C₄-C₄₀)alkyl, or (C₄-C₄₀)cycloalkyl. Furthermore, each R¹ is independently (C₄-C₄₀)alkyl or (C₄-C₄₀)cycloalkyl, each R² is independently (C₄-C₄₀)alkyl or (C₄-C₄)cycloalkyl, each R³ is independently (C₄-C₄₀)alkyl or (C₄-C₄₀)cycloalkyl, each R⁴ is independently (C₄-C₄)alkyl or (C₄-C₄₀)cycloalkyl, or each R⁵ is independently (C₄-C₄₀)alkyl or (C₄-C₄₀)cycloalkyl.

In one or more embodiments, each R¹ is independently (C₄-C₄₀)alkyl. In some embodiments, each R⁴ is (C₄-C₄₀)alkyl or each R² is (C₄-C₄₀)alkyl. In other embodiments, each R is independently (C₄-C₄₀)alkyl, and each R⁴ is (C₄-C₄₀)alkyl or each R² is (C₄-C₄₀)alkyl.

In one or more embodiments, each R¹, R², R³, R⁴, or R⁵ is optionally substituted [C₄]alkyl. The substituted [C₄]alkyl is substituted with one or more R^S, where each R^S is independently chosen from (C₁-C₂₀)alkyl or halogen.

In one or more embodiments, each R¹ is independently chosen from unsubstituted (C₅-C₂₀)alkyl, branched (C₅-C₂₀)alkyl, unsubstituted (C₆-C₂₀)alkyl, branched (C₆-C₂₀)alkyl, unsubstituted (C₅-C₈)alkyl, branched (C₅-C₈)alkyl, unsubstituted (C₈-C₃₀)alkyl, branched (C₈-C₃₀)alkyl or tallow alkyl. In some embodiments, each R¹ is independently chosen from 1,1-dimethylethyl (also called tert-butyl), n-butyl, 1-pentyl, 1-hexyl, heptyl, n-octyl, tert-octyl, nonyl, decyl, undecyl, or dodecyl. In other embodiments, R¹ is independently chosen from a linear (C₄-C₃₀)alkyl, a linear (C₅-C₃₀)alkyl, or branched (C₅-C₃₀)alkyl. In some embodiments, each R¹ is independently chosen from saturated [C₃₀]alkyl.

In one or more embodiments, each R², R³, R⁴ and R⁵ is —H.

In one or more embodiments of the catalyst system, the co-catalyst includes two cations selected from cations of formula (I). In some embodiments of the catalyst system, the co-catalyst includes two cations selected from cations of formula (II). In one or more embodiments, the co-catalyst includes two cations that are different from each other, and in other embodiments, the co-catalyst includes two cations that are the same.

In one or more embodiments, the co-catalyst has a solubility of greater than 20 milligrams per milliliter (mg/mL) in toluene at standard temperature and pressure (STP) (temperature of 22.5±2.5° C. and a pressure of approximately 1 atmosphere). In some embodiments, the co-catalyst has a solubility of from 20 to 100 mg/mL in toluene under STP. In other embodiments, the co-catalyst has a solubility of from 25 to 100 mg/mL in toluene under STP. All subranges in the range of from 20 to 100 mg/mL are included herein. All individual values and subranges from at least 20 to 100 mg/mL in toluene are included herein and disclosed herein as separate embodiments. For example, any one of the co-catalyst according to this disclosure may include at least 21 mg/mL; at least 25 mg/mL, or at least 30 mg/mL in toluene.

In one or more embodiments, the co-catalyst has a solubility of greater than 20 milligrams per milliliter (mg/mL) in methylcyclohexane (MCH) at standard temperature and pressure (STP) (temperature of 22.5±2.5° C. and a pressure of approximately 1 atmosphere). In some embodiments, the co-catalyst has a solubility of from 20 to 100 mg/mL in MCH under STP. All individual values and subranges from at least 20 to 100 mg/mL in MCH are included herein and disclosed herein as separate embodiments. For example, any one of the co-catalyst according to this disclosure may include at least 21 mg/mL; at least 25 mg/mL, or at least 30 mg/mL in MCH.

Solubility of a compound is determined at least in part by entropic effects in the solvent system. The entropic effects may include, for example, changes in lattice energy, solvation, solvent structure, or combinations thereof. Solvation is related to the interactions between a solute (such as an activator or co-catalyst) and molecules of the solvent. Without intending to be bound by theory, it is believed that increasing the number of carbon atoms in any one of each one of R¹, R², R³, R⁴, and R⁵ may, in turn, increase the solubility of the co-catalyst as a result of increase solvation. Additionally, it is believed that linear alkyl groups may render the co-catalyst more soluble in non-polar solvents than a branched alkyl groups in the same solvent, because the linear alkyl has a greater surface area than the branched alkyl. The increased surface area increases the solvent-solute interaction (i.e. solvation increases), thereby increasing the solubility of the linear alkyl in non-polar solvents, compared to the solubility of the branched alkyl in the same solvents.

Generally, a solute may have similar solubilities in different non-polar solvents. Non-polar solvents generally include hydrocarbon solvents. A non-limiting list of non-polar hydrocarbon solvents include: hexanes, cyclohexane, methylcyclohexane, heptanes, kerosene, toluene, xylenes, turpentine, and ISOPAR-E™ and combinations thereof. In the Example section, the co-catalysts, as described in this disclosure, sufficiently process polymers in a solvent system that includes methylcyclohexane or ISOPAR-E™, both of which are non-polar solvents, and more specifically are hydrocarbon solvents. Therefore, it is believed that the co-catalysts of this disclosure may sufficiently process polymers in other solvent systems.

In one or more embodiments, the catalyst system includes a catalyst, in which the catalyst is ionic. Not intending to be limiting, examples of the homogeneous catalysts include metallocene complexes, constrained geometry metal-ligand complexes (Li, H.; Marks, T. J., Proc. Natl. Acad. Sci. U.S.A. 2006, 103, 15295-15302; Li, H.; Li, L.; Schwartz, D. J.; Metz, M. V.; Marks, T. J.; Liable-Sands, L.; Rheingold, A. L., J. Am. Chem. Soc. 2005, 127, 14756-14768; McInnis, J. P.; Delferro, M.; Marks, T. J., Acc. Chem. Res. 2014, 47, 2545-2557; Delferro, M.; Marks, T. J., Chem. Rev. 2011, 111, 2450-2485.), pyridylamido Hf (or Zr, Ti) complexes (Arriola, D. J.; Carnahan, E. M.; Hustad, P. D.; Kuhlman, R. L.; Wenzel, T. T., Science, 2006, 312, 714-719.; Arriola, D. J.; Carnahan, E. M.; Cheung, Y. W.; Devore, D. D.; Graf, D. D.; Hustad, P. D.; Kuhlman, R. L.; Shan, C. L. P.; Poon, B. C.; Roof, G. R., U.S. Pat. No. 9,243,090 B2, 2016.), phenoxyimine metal complexes (Makio, H.; Terao, H.; Iwashita, A.; Fujita, T., Chem. Rev. 2011, 111, 2363-2449.), bis-biphenylphenoxy metal-ligand complexes (Arriola, D. J.; Bailey, B. C.; Klosin, J.; Lysenko, Z.; Roof, G. R.; Smith, A. J. WO2014209927A1, 2014.), etc. The following references summarize metal complexes as olefin polymerization catalysts both in industry and academia: Stürzel, M.; Mihan, S.; Mülhaupt, R., Chem. Rev. 2016, 116, 1398-1433.; Busico, V., Dalton Transactions 2009, 8794-8802.; Klosin, J.; Fontaine, P. P.; Figueroa, R., Acc. Chem. Res. 2015, 48, 2004-2016. All references listed in the detailed description of the present disclosure are incorporated herein.

Polyolefins

The catalytic systems described in the preceding paragraphs are utilized in the polymerization of olefins, primarily ethylene and propylene, to form ethylene-based polymers or propylene-based polymers. In some embodiments, there is only a single type of olefin or α-olefin in the polymerization scheme, creating a homopolymer. However, additional α-olefins may be incorporated into the polymerization procedure. The additional α-olefin co-monomers typically have no more than 20 carbon atoms. For example, the α-olefin co-monomers may have 3 to 10 carbon atoms or 3 to 8 carbon atoms. Exemplary α-olefin co-monomers include, but are not limited to, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, and 4-methyl-1-pentene. For example, the one or more α-olefin co-monomers may be selected from the group consisting of propylene, 1-butene, 1-hexene, and 1-octene; or in the alternative, from the group consisting of 1-hexene and 1-octene.

The ethylene-based polymers, for example homopolymers and/or interpolymers (including copolymers) of ethylene and optionally one or more co-monomers such as α-olefins, may comprise from at least 50 mole percent (mol %) monomer units derived from ethylene. All individual values and subranges encompassed by “from at least 50 mole percent” are disclosed herein as separate embodiments; for example, the ethylene-based polymers, homopolymers and/or interpolymers (including copolymers) of ethylene and optionally one or more co-monomers such as α-olefins may comprise at least 60 mole percent monomer units derived from ethylene; at least 70 mole percent monomer units derived from ethylene; at least 80 mole percent monomer units derived from ethylene; or from 50 to 100 mole percent monomer units derived from ethylene; or from 80 to 100 mole percent monomer units derived from ethylene.

In some embodiments, the polymerization process according to the present disclosure produces ethylene-based polymers. In one or more embodiments, the ethylene-based polymers may comprise at least 90 mole percent units derived from ethylene. All individual values and subranges from at least 90 mole percent are included herein and disclosed herein as separate embodiments. For example, the ethylene-based polymers may comprise at least 93 mole percent units derived from ethylene; at least 96 mole percent units; at least 97 mole percent units derived from ethylene; or in the alternative, from 90 to 100 mole percent units derived from ethylene; from 90 to 99.5 mole percent units derived from ethylene; or from 97 to 99.5 mole percent units derived from ethylene.

In some embodiments of the ethylene-based polymer, the amount of additional α-olefin is less than 50 mol %; other embodiments include at least 1 mole percent (mol %) to 25 mol %; and in further embodiments the amount of additional α-olefin includes at least 5 mol % to 103 mol %. In some embodiments, the additional α-olefin is 1-octene.

Any conventional polymerization processes may be employed to produce the ethylene-based polymers. Such conventional polymerization processes include, but are not limited to, solution polymerization processes, gas phase polymerization processes, slurry phase polymerization processes, and combinations thereof using one or more conventional reactors such as loop reactors, isothermal reactors, fluidized bed gas phase reactors, stirred tank reactors, batch reactors in parallel, series, or any combinations thereof, for example.

In one embodiment, the ethylene-based polymer may be produced via solution polymerization in a dual reactor system, for example a dual loop reactor system, wherein ethylene and optionally one or more α-olefins are polymerized in the presence of the catalyst system, as described herein, and optionally one or more co-catalysts. In another embodiment, the ethylene-based polymer may be produced via solution polymerization in a dual reactor system, for example a dual loop reactor system, wherein ethylene and optionally one or more C-olefins are polymerized in the presence of the catalyst system in this disclosure, and as described herein, and optionally one or more other catalysts. The catalyst system, as described herein, can be used in the first reactor, or second reactor, optionally in combination with one or more other catalysts. In one embodiment, the ethylene-based polymer may be produced via solution polymerization in a dual reactor system, for example a dual loop reactor system, wherein ethylene and optionally one or more α-olefins are polymerized in the presence of the catalyst system, as described herein, in both reactors.

In another embodiment, the ethylene-based polymer may be produced via solution polymerization in a single reactor system, for example a single loop reactor system, in which ethylene and optionally one or more α-olefins are polymerized in the presence of the catalyst system, as described within this disclosure, and optionally one or more co-catalysts, as described in the preceding paragraphs.

The ethylene-based polymers may further comprise one or more additives. Such additives include, but are not limited to, antistatic agents, color enhancers, dyes, lubricants, pigments, primary antioxidants, secondary antioxidants, processing aids, IV stabilizers, and combinations thereof. The ethylene-based polymers may contain any amounts of additives. The ethylene-based polymers may compromise from about 0 to about 10 percent by the combined weight of such additives, based on the weight of the ethylene-based polymers and the one or more additives. The ethylene-based polymers may further comprise fillers, which may include, but are not limited to, organic or inorganic fillers. The ethylene-based polymers may contain from about 0 to about 20 weight percent fillers such as, for example, calcium carbonate, tale or Mg(OH)₂, based on the combined weight of the ethylene-based polymers and all additives or fillers. The ethylene-based polymers may further be blended with one or more polymers to form a blend.

In some embodiments, a polymerization process for producing an ethylene-based polymer may include polymerizing ethylene and at least one additional α-olefin in the presence of a catalyst system according to the present disclosure. The polymer resulting from such a catalyst system that incorporates the metal-ligand complex of formula (I) may have a density according to ASTM D792 (incorporated herein by reference in its entirety) from 0.850 g/cm³ to 0.950 g/cm³, from 0.880 g/cm³ to 0.920 g/cm³, from 0.880 g/cm³ to 0.910 g/cm³, or from 0.880 g/cm³ to 0.900 g/cm³, for example.

In another embodiment, the polymer resulting from the catalyst system according to the present disclosure has a melt flow ratio (I₁₀/I₂) from 5 to 15, where the melt index, I2, is measured according to ASTM D1238 (incorporated herein by reference in its entirety) at 190° C. and 2.16 kg load and melt index I₁₀ is measured according to ASTM D1238 at 190° C. and 10 kg load. In other embodiments the melt flow ratio (I₁₀/I₂) is from 5 to 10, and in others, the melt flow ratio is from 5 to 9.

In some embodiments, the polymer resulting from the catalyst system according to the present disclosure has a molecular-weight distribution (MWD) from 1 to 25, where MWD is defined as M_w/M_n with M_w being a weight-average molecular weight and M_n being a number-average molecular weight. In other embodiments, the polymers resulting from the catalyst system have a MWD from 1 to 6. Another embodiment includes a MWD from 1 to 3; and other embodiments include MWD from 1.5 to 2.5.

Embodiments of the catalyst systems described in this disclosure yield unique polymer properties as a result of the high molecular weights of the polymers formed and the amount of the co-monomers incorporated into the polymers.

Ethylene Polymerization Experiments

Procedure for polymerization in toluene: In a typical experiment, a 150-mL glass pressure vessel (dried in a 120° C. oven overnight prior to use) was loaded with 40 mL of dry toluene inside the glovebox. A large magnetic stir bar was added to the pressure vessel, and it was sealed, taken out of the glovebox, and attached to a high-pressure/high-vacuum line. The pressure vessel was cooled to −78° C. with a dry ice/acetone bath and degassed, then allowed to warm and equilibrate at the desired reaction temperature for 30 min using an external bath. The solution was saturated with 1.0 atm of ethylene at the same time. The catalytically active species was freshly generated by mixing measured amounts of procatalyst and co-catalyst in a vial in the glovebox (10 mL of toluene) and shaking for 10 min. The catalyst solution was then removed from the glovebox and quickly injected into the rapidly stirring solution using a gastight syringe equipped with a spraying needle. The temperature of the toluene solution in representative polymerization experiments was monitored using a thermocouple. After a measured time interval, the polymerization was quenched by addition of 5 mL of MeOH. The solution was then reduced to ˜20 mL by removing the volatiles under vacuum. 100 mL of acidified MeOH (10% v/v HCl in MeOH) was then added, the polymer was stirred for several hours, filtered, washed with methanol and collected. It was then dried under high vacuum at 80° C. overnight to a constant weight.

Ethylene Copolymerization Experiments.

The procedure for ethylene and 1-hexene copolymerizations is similar to that for the ethylene homopolymerizations as previously described. A 350-mL glass pressure vessel is loaded with 40 mL of dry toluene and 10 mL of 1-hexene inside the glovebox. The procedures for catalyst preparation, injection into the polymerization flask, and copolymer workup are the same as previously described.

1-Octene Incorporation FTIR Analysis

The running of samples for the HT-GPC analysis precedes the IR analysis. For the IR analysis, a 48-well HT silicon wafer is utilized for deposition and analysis of 1-octene incorporation of samples. For the analysis, the samples are heated to 160° C. for less than or equal to 210 minutes; the samples are reheated to remove magnetic GPC stir bars and are shaken with glass-rod stir bars on a J-KEM Scientific heated robotic shaker. Samples are deposited while being heated using a Tecan MiniPrep 75 deposition station, and the 1,2,4-trichlorobenzene is evaporated off the deposited wells of the wafer at 160° C. under nitrogen purge. The analysis of 1-octene is performed on the HT silicon wafer using a NEXUS 670 E.S.P. FT-IR.

HT-GPC Analysis

The molecular weight data is determined by analysis on a hybrid Symyx/Dow built Robot-Assisted Dilution High-Temperature Gel Permeation Chromatographer (Sym-RAD-GPC). The polymer samples are dissolved by heating for 120 minutes at 160° C. in 1,2,4-trichlorobenzene (TCB) at a concentration of 10 mg/mL stabilized by 300 parts per million (ppm) of butylated hydroxyl toluene (BHT). Each sample is diluted to 1 mg/mL immediately before the injection of a 250 μL aliquot of the sample. The GPC is equipped with two Polymer Labs PLgel 10 μm MIXED-B columns (300×10 mm) at a flow rate of 2.0 mL/minute at 160° C. Sample detection is performed using a PolyChar IR4 detector in concentration mode. A conventional calibration of narrow polystyrene (PS) standards is utilized with apparent units adjusted to homo-polyethylene (PE) using known Mark-Houwink coefficients for PS and PE in TCB at this temperature.

2 L Parr Reactor Polymerization Procedure

The batch reactor polymerizations are conducted in a 2 L Parr batch reactor. The reactor is heated by an electrical heating mantle and is cooled by an internal serpentine cooling coil containing cooling water. Both the reactor and the heating/cooling system are controlled and monitored by a Camile™ TG process computer. The bottom of the reactor is fitted with a dump valve, which empties the reactor contents into a stainless-steel dump pot, which is prefilled with a catalyst kill solution (typically 5 mL of a Irgafos/Irganox/toluene mixture). The dump pot is vented to a 30 gal. blow-down tank, with both the pot and the tank purged with nitrogen. All solvents used for polymerization or catalyst makeup are run through solvent purification columns to remove any impurities that may affect polymerization. The 1-octene and IsoparE were passed through 2 columns, the first containing A2 alumina, the second containing Q5. The ethylene was passed through 2 columns, the first containing A204 alumina and 4 {acute over (Å)} mol sieves, the second containing Q5 reactant. The nitrogen gas, used for transfers, is passed through a single column containing A204 alumna, 4 {acute over (Å)} mol sieves and Q5.

The reactor is loaded first from the shot tank that may contain Isopar E solvent and/or 1-octene, depending on desired reactor load. The shot tank is filled to the load set points by use of a lab scale to which the shot tank is mounted. After liquid feed addition, the reactor is heated up to the polymerization temperature set point. Ethylene is added to the reactor when at reaction temperature to maintain reaction pressure set point. Ethylene addition amounts are monitored by a micro-motion flow meter.

The catalyst and activators were mixed with the appropriate amount of purified toluene to achieve a desired molarity solution. The catalyst and activators were handled in an inert glove box, drawn into a syringe and pressure transferred into the catalyst shot tank. This was followed by 3 rinses of toluene, 5 mL each. The run timer began immediately after catalyst addition from the shot take to the reactor. These polymerizations were run for 10 min., then the agitator was stopped, and the bottom dump valve opened to empty reactor contents to the dump pot. The dump pot contents are poured into trays placed in a lab hood where the solvent is evaporated off overnight. The trays containing the remaining polymer are then transferred to a vacuum oven, where they are heated up to 140° C. under vacuum to remove any remaining solvent. After the trays cool to ambient temperature, the polymers are weighed for yield and submitted for polymer testing.

Solubility Test Procedure

Solubility tests are performed at room temperature (22.5±2.5° C.). The chosen temperature is kept constant in all relevant parts of the equipment. A vial is charged with 30 mg of the co-catalyst (sample) and 1.0 mL of solvent. The suspension of co-catalyst and solvent is stirred for 30 minute at ambient temperature. Then, the mixture is filtered via a syringe filter into a tared vial and the solution is weighed (X g of solution). The solvent is next removed completely under high vacuum and the vial weighed again (Y g of sample). The “ρ_solvent” is the density of the solvent in g/mL. The solubility of co-catalyst in solvent was measured in units of mg/mL. The solubility of cocatalyst in solvent was calculated as follows:

$\begin{array}{cc}\mathrm{Solubility}=1000*Y*\frac{{\rho }_{sol\nu ent}}{X-Y}& \left(1\right)\end{array}$

One or more features of the present disclosure are illustrated in view of the examples as follows:

EXAMPLES

Examples 1 to 6 are synthetic procedures for intermediates and for isolated co-catalysts.

All manipulations of air-sensitive materials were performed with rigorous exclusion of O₂ and moisture in oven-dried Schlenk-type glassware on a dual manifold Schlenk line, interfaced to a high-vacuum line (10⁻⁶ Torr), or in a N₂-filled MBraun glove box with a high-capacity recirculator (<1 ppm O₂). Argon (Airgas, pre-purified grade) was purified by passage through a supported MnO oxygen-removal column and an activated Davison 4A molecular sieve column. Ethylene (Airgas) was purified by passage through an oxygen/moisture trap (Matheson, model MTRP-0042-XX). Hydrocarbon solvents (n-pentane, n-hexane, 1-hexene, methylcyclohexane, and toluene) were dried using activated alumina columns according to the method described by Grubbs (see Pangborn, A. B.; Giardello, M. A.; Grubbs, R. H.; Rosen, R. K.; Timmers, F. J., Safe and Convenient Procedure for Solvent Purification. Organometallics 1996, 15 (5), 1518-1520.) and were then vacuum-transferred from Na/K alloy. Benzene-d₆ and toluene-d₈ (Cambridge Isotope Laboratories, 99+ atom % D) were stored over Na/K alloy in vacuum and vacuum-transferred immediately prior to use. 1,2-Difluorobenzene and chlorobenzene-d₅ were dried with CaH₂, distilled under vacuum. Chloroform-d₃ and 1,1,2,2-tetrachloroethane-d₂ were used as received (Cambridge Isotope Laboratories, 99+ atom % D).

Synthesis of Compounds

Example 1: Synthesis of n-Octyl Trityl Alcohol

N-butyl lithium (11.5 mmol, 4.6 mL, 2.5 M in hexanes) was added slowly via syringe to a THF (50 mL) solution of p-octylbromobenzene (3.10 g, 11.5 mmol) at −78° C. The reaction was kept at −78° C. for 0.5 h. Next, Me₂CO₃ (0.33 g, 3.64 mmol, 0.31 mL) was added to the solution via syringe. The solution was then warmed to room temperature. After the solution was stirred overnight, water was added to the solution to quench the reaction. The mixture was extracted three times with Et₂O, and the organic extracts were combined and washed twice with brine, dried (Na₂SO₄), filtered, and concentrated to dryness. The resulting crude product was purified by flash column chromatography using basic aluminum oxide (activated, basic, Brockmann I, from Aldrich). Gradient elution (hexanes, hexanes/EtOAc=50/1, EtOAc) gave the pure product as colorless oil, 1.33 g, 58.1% yield.

¹H NMR (400 MHz, C₂D₂Cl₄) δ 7.36-7.10 (m, 12H), 2.71-2.57 (m, 6H), 1.67 (m, 6H), 1.44-1.25 (m, 30H), 1.02-0.85 (m, 9H). ¹³C NMR (151 MHz, C₂D₂Cl₄) δ 144.16, 141.63, 127.68, 127.63, 81.85 (Ar₃C, weak signal, confirmed by HMBC experiment), 35.42, 31.77, 31.28, 29.37, 29.32, 29.15, 22.60, 14.14. HR-MS (ESI) Calcd for C₄₃H₆₃ (M-OH)⁺: 579.4930, Found: 579.4946.

Example 2: Synthesis of n-Octyl Trityl Chloride

Acetyl chloride (0.265 g, 3.37 mmol, 0.24 mL) was added via syringe to a stirred solution of n-octyl trityl alcohol (0.67 g, 1.12 mmol) in toluene (20 mL) at 80° C. The reaction was kept at 80° C. for 1 h. All volatiles were removed, and the resulting oil product was further dried under high vacuum. The product light yellow oil was pure enough without further purification and a quantitative yield of 0.69 g.

¹H NMR (499 MHz, CDCl₃) δ 7.13 (m, 6H), 7.09 (m, 6H), 2.59 (m, 6H), 1.61 (m, 6H), 1.41-1.16 (m, 30H), 0.88 (m, 9H). ¹³C NMR (101 MHz, CDCl₃) δ 142.88, 142.41, 129.56, 127.58, 81.82 (Ar₃C, weak signal, confirmed by HMBC experiment), 35.52, 31.89, 31.26, 29.47, 29.40, 29.25, 22.67, 14.10. HR-MS (ESI) Calculated for C₄₃H₆₃ (M-Cl)⁺: 579.4930, Found: 579.4936

Example 3: Synthesis of Inventive Co-Catalyst 1

The dilithium salt (0.40 g, 0.30 mmol) (the synthesis was reported previously: Li, L.; Metz, M. V.; Li, H.; Chen, M.-C.; Marks, T. J.; Liable-Sands, L.; Rheingold, A. L., J. Am. Chem. Soc. 2002, 124, 12725-12741.) and n-octyl trityl chloride (0.37 g, 0.60 mmol) were mixed in toluene (30 mL) in Mbraun glovebox. After 3 hours, the solution was filtered through celite. Toluene was removed in vacuo and pentane (20 mL) was added. The pentane solution was stirred until a red oily mixture precipitated as solid. The solution was filtered to yield a red sticky solid. The solid was washed with pentane (1×20 mL). After drying under high vacuum, the product was collected as red solid. 0.42 g, 60% yield.

¹H NMR (500 MHz, CD₂Cl₂) δ 7.60 (d, J=8.0 Hz, 12H), 7.50 (d, J=8.0 Hz, 12H), 2.89 (t, J=7.8 Hz, 12H), 1.75 (m, 12H), 1.52-1.23 (m, 60H), 0.90 (t, J=6.6 Hz, 18H). ¹⁹F NMR (470 MHz, CD₂Cl₂) δ −130.99-−133.86 (m, 12F), −137.69 (m, 4F), −164.55-−165.15 (m, 6F), −166.95-−168.63 (m, 12F). HR-MS (ESI): [M-2Ar₃C]²⁻, 585.985 (found), 585.983 (calcd); [Ar₃C]⁺, 579.493 (found), 579.493 (calcd); [M-2Ar₃C—C₆F₅]⁻, 1004.974 (found), 1004.973 (calcd) [Ar=p-CH₃(CH₂)₇—C₆H₄—]. Elem. Anal. Calcd for C₁₂₈H₁₂₆B₂F₃₄: C, 65.93; H, 5.45; found: C, 66.01; H, 5.48.

Example 4: Synthesis of Inventive Co-Catalyst 2

The dilithium salt (0.29 g, 0.22 mmol) (the synthesis was reported previously: Li, L.; Metz, M. V.; Li, H.; Chen, M.-C.; Marks, T. J.; Liable-Sands, L.; Rheingold, A. L., J. Am. Chem. Soc. 2002, 124, 12725-12741.) and tert-butyl trityl chloride (0.20 g, 0.45 mmol, synthesized according to literature: S. Nakazawa et al., Angew. Chem., Int. Ed. 2012, 51, 9860-9864) were mixed in toluene (30 mL) in an Mbraun glovebox. After 3 hours, the solution was filtered through Celite. Toluene was removed in vacuo. The resulting mixture was then washed with a small amount of toluene. The resulting orange powder was dried under high vacuum. Single crystals suitable for X-ray diffraction were obtained from slow evaporation of toluene/1,2-difluorobenzene solution at room temperature. 0.16 g, 37% yield.

¹H NMR (500 MHz, CD₂Cl₂) δ 7.82 (d, J=8.6 Hz, 12H), 7.55 (d, J=8.5 Hz, 12H), 1.45 (s, 54H). ¹⁹F NMR (470 MHz, CD₂Cl₂) δ −131.08-−133.52 (m, 12F), −137.79 (m, 4F), −164.71-−165.20 (m, 6F), −167.28-−168.73 (m, 12F). HR-MS (ESI): [M-2Ar₃C]²⁻, 585.986 (found), 585.983 (calcd); [M-2Ar₃C—B(C₆F₅)₃+H]⁻, 660.990 (found), 660.987 (calcd). Elem. Anal. Calcd for C₁₀₄H₇₈B₂F₃₄: C, 62.60; H, 3.94; found: C, 62.85; H, 4.19.

Example 5: Synthesis of the Alkyl Ammonium Salt

Dilithium bis-borate salt (0.33 g, 0.25 mmol) and bis(hydrogenated tallow alkyl)dimethyl ammonium chloride (0.28 g, 0.49 mmol, the synthesis of which was reported previously: Rosen, R. K.; VanderLende, D. D., U.S. Pat. No. 5,919,983 A, 1999) were mixed in 30 mL of toluene in Mbraun glovebox for an hour. The toluene was removed under reduced pressure and 20 mL of pentane was added. The solution was filtered through Celite and the filtrate was dried under reduced pressure. The product was obtained as 0.49 g of a light-yellow oil, 89% yield.

¹H NMR (500 MHz, CD₂Cl₂) δ 8.77 (br, 1H), 2.98 (m, 8H), 2.72 (s, 6H), 1.73 (br, 8H), 1.28 (m, 120H), 0.89 (m, 12H). ¹⁹F NMR (470 MHz, CD₂Cl₂) δ −132.00-−133.81 (m, 12F), −138.00 (m, 4F), −162.96-−163.51 (m, 6F), −166.60-−167.80 (m, 12F).

The structures of the co-catalysts and catalysts that were investigated in the following examples are shown below.

Co-catalysts 1 and 2 have structures that include a non-coordinating borate dianion having the formula [(C₆F₅)₃B—C₆F₄—B(C₆F₅)₃]²⁻ and two cations, each cation according to formula (I) or formula (II). Comparative Co-catalysts C₂-C₃, which did not include a binuclear anion as recited in according to formula (I) or formula (II), were similarly assessed. R₂NMe in Inventive Co-catalyst 2 and Comparative co-catalyst C3 is bis(hydrogenated tallow alkyl)methylamine, i.e., di(n-octadecyl)methylamine. Co-catalysts' solubility, activity, and resulting polymer characteristics for the Co-catalysts 1 and 2 were assessed via the ethylene polymerization experiments, as previously described.

Single crystals of Inventive Co-catalyst 2 (Inventive 2) suitable for X-ray diffraction (XRD) studies were obtained upon slow evaporation of toluene/1,2-difluorobenzene (DFB) solutions at room temperature. As shown in the XRD structure of FIG. 1, the molecular structure included two trityl cations and one dianion. The distances between B1 and C24 and C24′ (the carbocation centers) are 7.329 Å and 5.637 Å, which indicates that the cation-anion interactions are non-covalent. The central carbon atoms of the trityl cations, C24 and C24′ are approximately sp₂ hybridized and lie in the plane that is defined by the —C₆F₄— group, with the trityl groups falling roughly perpendicular to that plane.

In the XRD structure of Inventive Co-catalyst 2 shown in FIG. 1, the fluorine atom in closest proximity to the trityl cation is labelled F12. The distance between F12 and C24′ is 3.235 Å. The distance is near the sum of van der Waals radii of carbon and fluorine atoms (3.17 Å). The distance between B1 and B1′ was measured at 6.211 Å. All of the bond angles of the boron atom and the four perfluorophenyl substituents were between 112.5° and 113.7°, thereby defining a borate anion with an approximate tetrahedral geometry. The tetrahedral geometry of the borate dianion prohibits the carbocations from forming close interactions with the borate anions, thereby creating very weakly coordinating anions.

In the ¹⁹F NMR spectrum of Inventive Co-catalyst 2 shown in FIG. 2, spectra (a) showed multiple signals for each type of —C₆F₄— fluorine atoms in the ¹⁹F NMR spectrum at room temperature for —C₆F₄— of B₂, t-Bu (in C₆D₅Cl). The multiple peaks indicate a restricted rotation barrier for the —C₆F₅ rings on each boron atom. Reorganization pathways available to Inventive Co-catalyst 2 were then examined using variable temperature ¹⁹F NMR spectroscopy. As the temperature was increased (spectra (c) and (d)), the two distinct signals converge into a single signal. The free energy of activation for —C₆F₅ reorganization (ΔG^#₃₆₃) was determined to be 17.9 kcal/mol based on a coalescence temperature of 363 K.

Solubility test results, as shown in Table 1, indicate that alkyl substitution on the trityl group significantly increase solubility in toluene at standard temperature and pressure, from Comparative C1 (approximately 0.0 mg/mL toluene) to Inventive Co-catalyst 1, an increase of more than 30 mg/mL toluene).

TABLE 1
Solubility of Binuclear Co-catalysts*
	Co-catalyst	Solvent	Solubility
	Inventive 1	Toluene	>30
	Inventive 3	Toluene	>30
	Comparative C1	Toluene	~0
	Inventive 1	MCH	>30
	Inventive 3	MCH	>30
	Comparative C1	MCH	~0
	*In units of mg of co-catalyst per mL of solvent. See solubility test procedure previously described.
	MCH = methylcyclohexane.

Polymerization reactions were carried out using rigorously anhydrous/anaerobic methodology with attention to exotherm and mass transfer effects as previously described. The ethylene homopolymerization and ethylene/1-hexene copolymerization results were summarized in Table 2, Table 3, and Table 4.

The conditions for Tables 2-4 were as follows: Procatalyst and co-catalyst were mixed for 10 minutes to form the catalyst system before injecting into reactor to start the polymerization reaction. When the catalyst was Zr₁, a 10 mol amount was included in the catalysts system, and when the catalyst system included Zr₂, 5 mol was added. An amount of mol was added when Comparative C2 was included in the catalyst system; alternatively, mol of Inventive Co-catalyst 1-2 or Comparative C1 was added to the catalyst system. The solvent in the polymerization reaction was either 45 mL of toluene or methylcyclohexane (MCH) or 43 mL of toluene and 2 mL of difluorobenzene (DFB). The ethylene pressure in the reactor was maintained at 1 atm. The temperature was 25° C., and the reaction time was 20 min unless otherwise specified. For Table 3 and Table 4, 5.0 mL of 1-hexene was added to the reactor.

TABLE 2
Ethylene Homocopolymerization Data of Procatalysts Zr2 and Zr1 and
Co-catalysts 1, C1 and C2 and Corresponding Branches in Polymers
						HMW		LMW
		Co-		poly.		(kg/mol);	wt %	(kg/mol);	wt %
	cat.	catalyst	solvent	(g)	act.b	PDIc	(HMW)	PDIc	(LMW)	Etd	Ld
1	Zr1	C2	T/DFB	1.14	342	315; 1.3	3	1; 1.1	97	1.6	4.2
2	Zr2	C1	T/DFB	0.210	63	238; 2.7	59	3; 2.4	41	3.6	0
3	Zr2	1	T/DFB	0.488	146	221; 2.0	41	2; 1.0	59	5.7	0
4	Zr2	2	T/DFB	0.394	118	190; 1.8	59	4; 1.2	41	4.6	0
5	Zr1	C2	T	1.147	344	—	0	1; 1.2	100	3.3	7.7
6	Zr2	C1	T	~0	~0e	—
7	Zr2	2	T	~0	~0e	—
8	Zr2	1	T	0.100	30	298; 2.3	92	2; 1.6	8	0	0
9	Zr1	C2	MCH	~0	~0e	—
10	Zr2	C1	MCH	~0	~0e	—
11	Zr2	2	MCH	~0	~0e	—
12	Zr2	1	MCH	0.062	19	315; 8.5	100	—	—	0	0
bUnit is (kg polymer) · (mol of metal)−1 · h−1 · atm−1.
cDetermined by GPC against polystyrene standards in (g · mol−1).
dNumbers of branches per 1000 carbon atoms calculated from the integration of 13C NMR resonances. Branching assigned according to literature (Galland, G. B.; De Souza, R. F.; Mauler, R. S.; Nunes, F. F., Macromolecules 1999, 32, 1620-1625; Jung, M.; Lee, Y.; Kwak, S.; Park, H.; Kim, B.; Kim, S.; Lee, K. H.; Cho, H. S.; Hwang, K. Y., Anal. Chem. 2016, 88, 1516-1520.)
Et: ethyl branches,
Bu: n-butyl branches,
L = long chain branches with ≥6 carbons.

TABLE 3
Ethylene/1-hexene Copolymerization Data of Procatalysts Zr2 and
Zr1 and Co-catalysts 1 and Corresponding Branches in Polymers
						HMW		LMW
		co-		poly.		(kg/mol);	wt %	(kg/mol);	wt %
entry	cat.	catalyst	solvent	(g)	act.b	PDIc	(HMW)	PDIc	(LMW)	Etd	Bud
1	Zr2	C1	T/DFB	0.670	201	99; 1.7	25	2; 1.6	75	8.8	79.7
2	Zr2	1	T/DFB	0.440	132	96; 2.1	15	2; 1.0	85	8.2	70.0
3	Zr1	C2	T	0.430	139	—	0	1; 1.1	100	6.1	33.3
4	Zr2	1	T	0.180	54	125; 1.9	53	4; 1.4	47	5.3	78.1
5	Zr2	1	MCH	0.084	25	113; 1.9	93	2; 1.0	7	0	93.7
bUnit is (kg polymer) · (mol of metal)−1 · h−1 · atm−1.
dDetermined by GPC against polystyrene standards in (g · mol−1).
dNumbers of branches per 1000 Carbon calculated from the integration of 13C NMR resonances. Branching assigned according to literature (Galland, G. B.; De Souza, R. F.; Mauler, R. S.; Nunes, F. F., Macromolecules 1999, 32, 1620-1625; Jung, M.; Lee, Y.; Kwak, S.; Park, H.; Kim, B.; Kim, S.; Lee, K. H.; Cho, H. S.; Hwang, K. Y., Anal. Chem. 2016, 88, 1516-1520.)
Et: ethyl branches,
Bu: n-butyl branches,
L = long chain branches with ≥6 carbons.

The data summarized in Table 2 and Table 3 showed that in toluene and DFB, both Inventive Co-catalyst 1 and Inventive Co-catalyst 2 exhibited higher ethylene homopolymerization activities over Comparative C. Comparative C1 showed no activity in the absence of DFB, whereas Inventive Co-catalyst 1 showed activity in toluene and methylcyclohexane (MCH) for both ethylene homopolymerization and ethylene-1-hexene copolymerizations. In toluene and DFB, both Comparative C2 and Inventive Co-catalyst 1 showed similar activity, with similar product molecular weight, PDI, and n-butyl branching, indicating the more soluble Inventive Co-catalyst 1 has no detrimental effect on the catalytic polymerization. In toluene, Inventive Co-catalyst 1 produced higher molecular weight product with enhanced n-butyl branching (51.9%, Table 2) in comparison to when 2 equivalents of Comparative C2 are used (21.2%, Table 2), indicating the cooperative effects of Inventive 1 on the bis-cationic polymerization catalysis.

TABLE 4
Ethylene/1-Hexene Copolymerization Resultsa
			t		HMW	wt %	LMW	wt %
Co-catalyst	Catalyst	Solvent	min	Act.b	PDIc	HMW	PDIc	LMW	Etd	Bud	Ld
1	C3	Zr1	T/DFB	20	8	245; 2.8	88	3; 1.6	12	0	32.3	0
2	3	Zr2	T/DFB	40	10	129; 2.0	96	3; 1.1	4	5.5	78.1	7.6
3	C3	Zr1	T	20	11	359; 5.9	77	2; 1.0	23	0	26.1	0
4	3	Zr2	T	40	8	163; 2.3	97	1; 1.0	3	0	70.0	5.6
5	C3	Zr1	MCH	20	7	261; 4.7	95	2; 1.0	5	0	45.7	0
6	3	Zr2	MCH	40	10	61; 2.6	100	/	0	0	97.3	6.2
bUnit is (kg polymer) · (mol of metal)−1 · h−1 · atm−1.
cDetermined by GPC against polystyrene standards in kg · mol−1 (low-Mw samples that have a low polydispersity pattern likely reflects imprecision in calibration).
dNumbers of branches per 1000 Carbon calculated from the integration of 13C NMR resonances. Branching assigned according to literature (Galland, G. B.; De Souza, R. F.; Mauler, R. S.; Nunes, F. F., Macromolecules 1999, 32, 1620-1625; Jung, M.; Lee, Y.; Kwak, S.; Park, H.; Kim, B.; Kim, S.; Lee, K. H.; Cho, H. S.; Hwang, K. Y., Anal. Chem. 2016, 88, 1516-1520.)
Et: ethyl branches,
Bu: n-butyl branches,
L = long chain branches with ≥6 carbons.

The data in Table 4 show that the polymer produced by the catalyst system containing Inventive Co-catalyst 3 exhibits higher branching densities than the catalyst system containing Comparative Co-catalyst C3.

TABLE 5
Ethylene/1-octene copolymerization with Procatalysts A, B, C, Zr2 and
Ti1 and Inventive Co-catalysts 1 and 3 at 120° C. in a 2 L Parr reactor
		Catalyst		Activator				1-Octene
		loading	Co-	Loading	Yield	Mw		incorporation
Entry	Catalyst	(μmol)	catalyst	(μmol)	(g)	(g/mol)	PDI	(mol %)
1	A	1.0	3	1.2	21.2	564,000	2.1	0.7
2	A	1.0	3	0.6	22.7	573,000	2.1	0.6
3	B	0.4	3	0.48	46.8	52,000	2.3	26.8
4	B	0.4	3	0.24	30.3	54,000	2.3	27.6
5	B	0.1	1	0.50	17.9	46,000	2.2	27.5
6	C	0.15	3	0.075	5.3	861,000	3.5	17.9
7	Zr2	1.2	1	1.2	9.1	14,000	19.4	9.9
8	Ti1	0.5	3	0.25	14.4	61,000	2.2	19.7
9	Ti1	0.6	1	0.30	43.4	64,000	2.6	20.5
10	Ti2	0.6	3	0.6	27.2	126,000	3.6	25.6
11	Ti2	0.6	1	0.6	34.4	93,000	4.1	24.9

Conditions: 120° C., 270 psig, 611 g Isopar E, 300 g 1-octene in a 2 L Parr reactor, 10-minute reaction time, 1-octene incorporation measured by FTIR, Mw and PDI measured by HT-GPC

The results summarized in Table 5 demonstrate that Inventive Co-catalyst 3 activates both Procatalyst A and Procatalyst B for olefin polymerization at elevated temperature and pressure in the hydrocarbon solvent Isopar E.

Equipment Standards

All solvents and reagents are obtained from commercial sources and used as received unless otherwise noted. Anhydrous toluene, hexanes, tetrahydrofuran, and diethyl ether are purified via passage through activated alumina and, in some cases, Q-5 reactant. Solvents used for experiments performed in a nitrogen-filled glovebox are further dried by storage over activated 4 Å molecular sieves. Glassware for moisture-sensitive reactions is dried in an oven overnight prior to use. NMR spectra are recorded on Varian 400-MR and VNMRS-500 spectrometers. LC-MS analyses are performed using a Waters e2695 Separations Module coupled with a Waters 2424 ELS detector, a Waters 2998 PDA detector, and a Waters 3100 ESI mass detector. LC-MS separations are performed on an XBridge C18 3.5 m 2.1×50 mm column using a 5:95 to 100:0 acetonitrile to water gradient with 0.1% formic acid as the ionizing agent. HRMS analyses are performed using an Agilent 1290 Infinity LC with a Zorbax Eclipse Plus C18 1.8 m 2.1×50 mm column coupled with an Agilent 6230 TOF Mass Spectrometer with electrospray ionization. H NMR data are reported as follows: chemical shift (multiplicity (br=broad, s=singlet, d=doublet, t=triplet, q=quartet, p=pentet, sex=sextet, sept=septet and m=multiplet), integration, and assignment). Chemical shifts for ¹H NMR data are reported in ppm downfield from internal tetramethylsilane (TMS, δ scale) using residual protons in the deuterated solvent as references. ¹³C NMR data are determined with ¹H decoupling, and the chemical shifts are reported downfield from tetramethylsilane (TMS, δ scale) in ppm versus the using residual carbons in the deuterated solvent as references.

Claims

1. A catalyst system comprising: a procatalyst; anda co-catalyst dissolved in a non-halogenated solvent, the co-catalyst comprising: a non-coordinating borate dianion having the formula:

2. The catalyst system according to claim 1, wherein the procatalyst upon activation is ionic.

3. The catalyst system according to claim 1, wherein each R1 is independently (C4-C30)alkyl.

4. The catalyst system according to claim 1, wherein each R1 is independently tert-butyl, n-butyl, tert-octyl, or n-octyl.

5. The catalyst system according to claim 1, wherein each R2, R3, R4 and R5 is —H.

6. The catalyst system according to claim 1, wherein each R1 is independently chosen from n-butyl, tert-butyl, 1-pentyl, 1-hexyl, heptyl, n-octyl, nonyl, decyl, undecyl, or dodecyl.

7. The catalyst system according to claim 1, wherein each R1 is independently chosen from a linear (C4-C30)aticyl or a linear or branched (C5-C30)alkyl.

8. The catalyst system according to claim 1, wherein the two cations are both selected from cations according to formula (I).

9. The catalyst system according to claim 1, wherein one of the two cations is selected from formula (I) and the other of the cations is selected from formula (II).

10. The catalyst system according to claim 1, wherein the co-catalyst has a solubility of greater than 20 milligrams per milliliter (mg/mL) in toluene under conditions of 25° C. and 1 atmosphere.

11. A polymerization process for producing ethylene-based polymer, the process comprising: polymerizing ethylene and optionally one or more α-olefins in the presence of a catalyst system, the catalyst system comprising a procatalyst and a co-catalyst dissolved in a non-halogenated aprotic hydrocarbon solvent, wherein the co-catalyst comprises: a non-coordinating borate dianion having the formula:

12. The process according to claim 11, wherein the α-olefin is 1-octene.

13. The process according to claim 11, wherein the non-halogenated solvent is toluene or an aliphatic solvent.

14. The process according to claim 11, wherein each R1 is independently tert-butyl, n-butyl, tert-octyl, or n-octyl.

15. The process according to claim 11, wherein each R2, R3, R4 and R5 is —H.

16. The process according to claim 11, wherein the two cations are both selected from cations according to formula (I).

17. The process according to claim 11, wherein one of the two cations is selected from formula (I) and the other of the cations is selected from formula (II).