US20160362510A1 - Method to prepare ethylene copolymers - Google Patents

Method to prepare ethylene copolymers Download PDF

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Publication number
US20160362510A1
US20160362510A1 US15/118,014 US201515118014A US2016362510A1 US 20160362510 A1 US20160362510 A1 US 20160362510A1 US 201515118014 A US201515118014 A US 201515118014A US 2016362510 A1 US2016362510 A1 US 2016362510A1
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group
divalent
catalyst
substituted
canceled
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Francis C. Rix
Ching-Tai Lue
C. Jeff Harlan
Laughlin G. McCullough
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Univation Technologies LLC
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Univation Technologies LLC
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    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
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    • B32—LAYERED PRODUCTS
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    • C08F2420/12—Long bridge, i.e. Cp or analog where the bridging unit linking the two Cps or analogs is composed of at least two atoms which are not part of a cycle and which are not an ethylene bridge
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    • C08L23/04—Homopolymers or copolymers of ethene
    • C08L23/08—Copolymers of ethene
    • C08L23/0807—Copolymers of ethene with unsaturated hydrocarbons only containing more than three carbon atoms
    • C08L23/0815—Copolymers of ethene with aliphatic 1-olefins
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • Ethylene alpha-olefin (polyethylene) copolymers are typically produced in a low pressure reactor, utilizing, for example, solution, slurry, or gas phase polymerization processes. Polymerization takes place in the presence of catalyst systems such as those employing, for example, a Ziegler-Natta catalyst, a chromium based catalyst, a metallocene catalyst, or combinations thereof.
  • catalyst systems such as those employing, for example, a Ziegler-Natta catalyst, a chromium based catalyst, a metallocene catalyst, or combinations thereof.
  • a number of catalyst compositions containing single site, e.g., metallocene, catalysts have been used to prepare polyethylene copolymers, producing relatively homogeneous copolymers at good polymerization rates.
  • single site catalyst compositions such as metallocene catalysts
  • Single site catalysts are catalytic compounds in which each catalyst molecule contains one or only a few polymerization sites.
  • Single site catalysts often produce polyethylene copolymers that have a narrow molecular weight distribution. Although there are single site catalysts that can produce broader molecular weight distributions, these catalysts often show a narrowing of the molecular weight distribution as the reaction temperature is increased, for example, to increase production rates.
  • a single site catalyst will often incorporate comonomer among the molecules of the polyethylene copolymer at a relatively uniform rate. The molecular weight distribution and the amount of comonomer incorporation can be used to determine a composition distribution.
  • composition distribution of an ethylene alpha-olefin copolymer refers to the distribution of comonomer, which form short chain branches, among the molecules that comprise the polyethylene polymer.
  • the resin is said to have a “broad” composition distribution.
  • the amount of comonomer per 1000 carbons is similar among the polyethylene molecules of different chain lengths, the composition distribution is said to be “narrow”.
  • composition distribution is known to influence the properties of copolymers, for example, stiffness, toughness, extractable content, environmental stress crack resistance, and heat sealing, among other properties.
  • the composition distribution of a polyolefin may be readily measured by methods known in the art, for example, Temperature Raising Elution Fractionation (TREF) or Crystallization Analysis Fractionation (CRYSTAF).
  • Resins having a broad orthogonal composition distribution in which the comonomer is incorporated predominantly in the high molecular weight chains can lead to improved physical properties, for example toughness properties and environmental stress crack resistance (ESCR). Because of the improved physical properties of resins with orthogonal composition distributions needed for commercially desirable products, there exists a need for controlled techniques for forming polyethylene copolymers having a broad orthogonal composition distribution.
  • BOCD broad orthogonal composition distribution
  • ESCR environmental stress crack resistance
  • An exemplary embodiment described herein provides a method of polymerizing olefins to produce a polyolefin polymer with a multimodal composition distribution, including contacting ethylene and a comonomer with a catalyst system.
  • the catalyst system includes a first catalyst compound and a second catalyst compound that are co-supported to form a commonly supported catalyst system.
  • the first catalyst compound includes a compound with the following formula:
  • each R 1 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • each R 2 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • at least one R 1 and at least one R 2 is a hydrocarbyl or substituted hydrocarbyl group; adjacent groups R 1 and R 2 groups may be coupled to form a ring;
  • each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group, or a divalent radical that links to an R 1 or R 2 group.
  • the second catalyst compound includes at least one of the following formulas:
  • each R 3 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • R 4 is a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • each R 5 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • R 3 , R 4 , and R 5 may be the same or different
  • R 3 , R 4 , or R 5 groups may be joined with R 3 , R 4 , or R 5 groups on an opposing cyclopentadienyl structure to form one or more bridges if the number of atoms connecting the two cyclopentadienyl rings is ⁇ 3
  • each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group.
  • Another embodiment provides a catalyst composition including a first catalyst compound and a second catalyst compound that are co-supported forming a commonly supported catalyst system.
  • the first catalyst compound includes a compound with the following formula:
  • each R 1 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • each R 2 is independently a H, hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • at least one R 1 and at least one R 2 is a hydrocarbyl or substituted hydrocarbyl group; adjacent groups R 1 and R 2 groups may be coupled to form a ring;
  • each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group, or a divalent radical that links to an R 1 or R 2 group.
  • the second catalyst compound includes at least one of the following formulas:
  • each R 3 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • R 4 is a hydrocarbyl group, a substituted hydrocarbyl group, or a heteoatom group
  • each R 5 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group
  • R 3 , R 4 , and R 5 may be the same or different
  • R 3 , R 4 , or R 5 groups may be joined with R 3 , R 4 , or R 5 groups on an opposing cyclopentadienyl structure to form one or more bridges if the number of atoms connecting the two cyclopentadienyl rings is ⁇ 3
  • each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group.
  • X may be a divalent radical that links to a R 3 , R 4 , or
  • FIG. 1 is a schematic of a gas-phase reactor system, showing the addition of at least two catalysts, at least one of which is added as a trim catalyst.
  • FIG. 2 is a plot of a series of polymers that were prepared to test the relative abilities of a series of metallocene catalysts to prepare a resin having about a 1 melt index (MI) and a density (D) of about 0.92.
  • MI melt index
  • D density
  • FIG. 3 is a plot of the series of polymers of FIG. 2 , showing the melt index ratio (MIR) of the series of polymers made by different metallocene (MCN) catalysts.
  • MIR melt index ratio
  • FIG. 4 is a flow chart of a method for making a co-supported polymerization catalyst.
  • a pre-catalyst is a catalyst compound prior to exposure to activator.
  • LLDPE linear low-density polyethylene film
  • an ethylene hexene copolymer with a molecular weight of between about 90 Kg/mol and 110 Kg/mol, or about 100 Kg/mol and an average density of between about 0.9 and 0.925, or about 0.918.
  • the typical MWD for linear metallocene resins is 2.5-3.5.
  • Blend studies indicate that it would be desirable to broaden this distribution by employing two catalysts that each provides different average molecular weights.
  • the ratio of the Mw for the low molecular weight component and the high molecular weight component would be between 1:1 and 1:10, or about 1:2 and 1:5.
  • the density of a polyethylene copolymer provides an indication of the incorporation of comonomer into a polymer, with lower densities indicating higher incorporation.
  • the difference in the densities of the low molecular weight (LMW) component and the high molecular weight (HMW) component would preferably be greater than about 0.02, or greater than about 0.04 with the HMW component having a lower density than the LMW component.
  • LMW low molecular weight
  • HMW high molecular weight
  • the difference in density requires around around around a 1.5:1 or preferably about 2:1, or more preferably about 3:1 or more preferably a 4:1 or even a greater than 4:1 difference difference in comonomer incorporation ability.
  • LCB long chain branching
  • MWD and SCBD can be adjusted by changing the relative amount of the two pre-catalysts on the support. This may be adjusted during the formation of the pre-catalysts, for example, by supporting two catalysts on a single support.
  • the relative amounts of the pre-catalysts can be adjusted by adding one of the components to a catalyst mixture en-route to the reactor in a process termed “trim.” Feedback of polymer property data can be used to control the amount of catalyst addition.
  • MNs Metallocenes
  • a variety of resins with different MWD, SCBD, and LCBD may be prepared from a limited number of catalysts.
  • the pre-catalysts should trim well onto activator supports. Two parameters that benefit this are solubility in alkane solvents and rapid supportation on the catalyst slurry en-route to the reactor. This favors the use of MCNs to achieve controlled MWD, SCBD, and LCBD. Techniques for selecting catalysts that can be used to generate targeted molecular weight compositions, including BOCD polymer systems, are disclosed herein.
  • the first section discusses catalyst compounds that can be used in embodiments.
  • the second section discusses generating catalyst slurrys that may be used for implementing the techniques described.
  • the third section discusses catalyst supports that may be used.
  • the fourth section discusses catalyst activators that may be used.
  • the fifth section discusses the catalyst component solutions that may be used to add additional catalysts in trim systems.
  • Gas phase polymerizations may use static control or continuity agents, which are discussed in the sixth section.
  • a gas-phase polymerization reactor with a trim feed system is discussed in the seventh section.
  • the use of the catalyst composition to control product properties is discussed in an eighth section and an exemplary polymerization process is discussed in a ninth section. Examples of the implementation of the procedures discussed is incorporated into a tenth section.
  • Metallocene catalyst compounds can include “half sandwich” and/or “full sandwich” compounds having one or more Cp ligands (cyclopentadienyl and ligands isolobal to cyclopentadienyl) bound to at least one Group 3 to Group 12 metal atom, and one or more leaving group(s) bound to the at least one metal atom.
  • the Cp ligands are one or more rings or ring system(s), at least a portion of which includes i-bonded systems, such as cycloalkadienyl ligands and heterocyclic analogues.
  • the ring(s) or ring system(s) typically include atoms selected from the group consisting of Groups 13 to 16 atoms, and, in a particular exemplary embodiment, the atoms that make up the Cp ligands are selected from the group consisting of carbon, nitrogen, oxygen, silicon, sulfur, phosphorous, germanium, boron, aluminum, and combinations thereof, where carbon makes up at least 50% of the ring members.
  • the Cp ligand(s) are selected from the group consisting of substituted and unsubstituted cyclopentadienyl ligands and ligands isolobal to cyclopentadienyl, non-limiting examples of which include cyclopentadienyl, indenyl, fluorenyl and other structures.
  • Such ligands include cyclopentadienyl, cyclopentaphenanthreneyl, indenyl, benzindenyl, fluorenyl, octahydrofluorenyl, cyclooctatetraenyl, cyclopentacyclododecene, phenanthrindenyl, 3,4-benzofluorenyl, 9-phenylfluorenyl, 8-H-cyclopent[a]acenaphthylenyl, 7-H-dibenzofluorenyl, indeno[1,2-9]anthrene, thiophenoindenyl, thiophenofluorenyl, hydrogenated versions thereof (e.g., 4,5,6,7-tetrahydroindenyl, or “H 4 Ind”), substituted versions thereof (as discussed and described in more detail below), and heterocyclic versions thereof.
  • H 4 Ind hydrogenated versions thereof
  • the metal atom “M” of the metallocene catalyst compound can be selected from the group consisting of Groups 3 through 12 atoms and lanthanide Group atoms in one exemplary embodiment; and selected from the group consisting of Groups 3 through 10 atoms in a more particular exemplary embodiment, and selected from the group consisting of Sc, Ti, Zr, Hf, V, Nb, Ta, Mn, Re, Fe, Ru, Os, Co, Rh, Ir, and Ni in yet a more particular exemplary embodiment; and selected from the group consisting of Groups 4, 5, and 6 atoms in yet a more particular exemplary embodiment, and Ti, Zr, Hf atoms in yet a more particular exemplary embodiment, and Hf in yet a more particular exemplary embodiment.
  • the oxidation state of the metal atom “M” can range from 0 to +7 in one exemplary embodiment; and in a more particular exemplary embodiment, can be +1, +2, +3, +4, or +5; and in yet a more particular exemplary embodiment can be +2, +3 or +4.
  • the groups bound to the metal atom “M” are such that the compounds described below in the formulas and structures are electrically neutral, unless otherwise indicated.
  • the Cp ligand forms at least one chemical bond with the metal atom M to form the “metallocene catalyst compound.”
  • the Cp ligands are distinct from the leaving groups bound to the catalyst compound in that they are not highly susceptible to substitution/abstraction reactions.
  • the one or more metallocene catalyst compounds can be represented by the formula (I):
  • the ligands represented by Cp A and Cp B in formula (I) can be the same or different cyclopentadienyl ligands or ligands isolobal to cyclopentadienyl, either or both of which can contain heteroatoms and either or both of which can be substituted by a group R.
  • Cp A and Cp B are independently selected from the group consisting of cyclopentadienyl, indenyl, tetrahydroindenyl, fluorenyl, and substituted derivatives of each.
  • each Cp A and Cp B of formula (I) can be unsubstituted or substituted with any one or combination of substituent groups R.
  • substituent groups R as used in structure (I) as well as ring substituents in structures Va-d, discussed and described below, include groups selected from the group consisting of hydrogen radicals, alkyls, alkenyls, alkynyls, cycloalkyls, aryls, acyls, aroyls, alkoxys, aryloxys, alkylthiols, dialkylamines, alkylamidos, alkoxycarbonyls, aryloxycarbonyls, carbomoyls, alkyl- and dialkyl-carbamoyls, acyloxys, acylaminos, aroylaminos, and combinations thereof.
  • alkyl substituents R associated with formulas (I) through (Va-d) include methyl, ethyl, propyl, butyl, pentyl, hexyl, cyclopentyl, cyclohexyl, benzyl, phenyl, methylphenyl, and tert-butylphenyl groups and the like, including all their isomers, for example, tertiary-butyl, isopropyl, and the like.
  • hydrocarbyl substituents, or groups are made up of between 1 and 100 or more carbon atoms, the remainder being hydrogen.
  • Non-limiting examples of hydrocarbyl substituents include linear or branched or cyclic: alkyl radicals; alkenyl radicals; alkynyl radicals; cycloalkyl radicals; aryl radicals; alkylene radicals, or a combination thereof.
  • Non-limiting examples include methyl, ethyl, propyl, butyl, pentyl, hexyl, cyclopentyl, cyclohexyl; olefinically unsaturated substituents including vinyl-terminated ligands (for example but-3-enyl, prop-2-enyl, hex-5-enyl and the like), benzyl or phenyl groups and the like, including all their isomers, for example tertiary butyl, isopropyl, and the like.
  • substituted hydrocarbyl substituents, or groups are made up of between 1 and 100 or more carbon atoms, the remainder being hydrogen, fluorine, chlorine, bromine, iodine, oxygen, sulfur, nitrogen, phosphorous, boron, silicon, germanium or tin atoms or other atom systems tolerant of olefin polymerization systems.
  • Substituted hydrocarbyl substituents are carbon based radicals.
  • Non-limiting examples of substituted hydrocarbyl substituents trifluoromethyl radical, trimethylsilanemethyl (Me3SiCH 2 ⁇ ) radicals.
  • heteroatom substituents are fluorine, chlorine, bromine, iodine, oxygen, sulfur, nitrogen, phosphorous, boron, silicon, germanium or tin based radicals. They may be the heteroatom atom by itself Further, heteroatom substituents include organometalloid radicals.
  • heteroatom substituents include chloro radicals, fluoro radicals, methoxy radicals, diphenyl amino radicals, thioalkyls, thioalkenyls, trimethylsilyl radicals, dimethyl aluminum radicals, alkoxydihydrocarbylsilyl radicals, siloxydiydrocabylsilyl radicals, tris(perflourophenyl)boron and the like.
  • radicals include substituted alkyls and aryls such as, for example, fluoromethyl, fluroethyl, difluroethyl, iodopropyl, bromohexyl, chlorobenzyl, hydrocarbyl substituted organometalloid radicals including trimethylsilyl, trimethylgermyl, methyldiethylsilyl, and the like, and halocarbyl-substituted organometalloid radicals, including tris(trifluoromethyl)silyl, methylbis(difluoromethyl)silyl, bromomethyldimethylgermyl and the like; and disubstituted boron radicals including dimethylboron, for example; and disubstituted Group 15 radicals including dimethylamine, dimethylphosphine, diphenylamine, methylphenylphosphine, as well as Group 16 radicals including methoxy, ethoxy, propoxy, phenoxy, methyl
  • substituent groups R include, but are not limited to, olefins such as olefinically unsaturated substituents including vinyl-terminated ligands such as, for example, 3-butenyl, 2-propenyl, 5-hexenyl, and the like.
  • olefins such as olefinically unsaturated substituents including vinyl-terminated ligands such as, for example, 3-butenyl, 2-propenyl, 5-hexenyl, and the like.
  • at least two R groups are joined to form a ring structure having from 3 to 30 atoms selected from the group consisting of carbon, nitrogen, oxygen, phosphorous, silicon, germanium, aluminum, boron, and combinations thereof.
  • a substituent group R such as 1-butanyl can form a bonding association to the element M.
  • Each X in the formula (I) above and for the formula/structures (II) through (Va-d) below is independently selected from the group consisting of: any leaving group, in one exemplary embodiment; halogen ions, hydrides, C 1 to C 12 alkyls, C 2 to C 12 alkenyls, C 6 to C 12 aryls, C 7 to C 20 alkylaryls, C 1 to C 12 alkoxys, C 6 to C 16 aryloxys, C 7 to C 8 alkylaryloxys, C 1 to C 12 fluoroalkyls, C 6 to C 12 fluoroaryls, and C 1 to C 12 heteroatom-containing hydrocarbons and substituted derivatives thereof, in a more particular exemplary embodiment; hydride, halogen ions, C 1 to C 6 alkyls, C 2 to C 6 alkenyls, C 7 to C 18 alkylaryls, C 1 to C 6 alkoxys, C 6 to C 14 aryloxys, C 7 to
  • X groups include amines, phosphines, ethers, carboxylates, dienes, hydrocarbon radicals having from 1 to 20 carbon atoms, fluorinated hydrocarbon radicals (e.g., —C 6 F 5 (pentafluorophenyl)), fluorinated alkylcarboxylates (e.g., CF 3 C(O)O ⁇ ), hydrides, halogen ions and combinations thereof.
  • fluorinated hydrocarbon radicals e.g., —C 6 F 5 (pentafluorophenyl)
  • fluorinated alkylcarboxylates e.g., CF 3 C(O)O ⁇
  • hydrides halogen ions and combinations thereof.
  • X ligands include alkyl groups such as cyclobutyl, cyclohexyl, methyl, heptyl, tolyl, trifluoromethyl, tetramethylene, pentamethylene, methylidene, methyoxy, ethyoxy, propoxy, phenoxy, bis(N-methylanilide), dimethylamide, dimethylphosphide radicals and the like.
  • two or more X's form a part of a fused ring or ring system.
  • X can be a leaving group selected from the group consisting of chloride ions, bromide ions, C 1 to C 10 alkyls, and C 2 to C 12 alkenyls, carboxylates, acetylacetonates, and alkoxides.
  • the metallocene catalyst compound includes those of formula (I) where Cp A and Cp B are bridged to each other by at least one bridging group, (A), such that the structure is represented by formula (II):
  • bridged metallocenes These bridged compounds represented by formula (II) are known as “bridged metallocenes.”
  • the elements Cp A , Cp B , M, X and n in structure (II) are as defined above for formula (I); where each Cp ligand is chemically bonded to M, and (A) is chemically bonded to each Cp.
  • the bridging group (A) can include divalent hydrocarbon groups containing at least one Group 13 to 16 atom, such as, but not limited to, at least one of a carbon, oxygen, nitrogen, silicon, aluminum, boron, germanium, tin atom, and combinations thereof; where the heteroatom can also be C 1 to C 12 alkyl or aryl substituted to satisfy neutral valency.
  • the bridging group (A) can also include substituent groups R as defined above (for formula (I)) including halogen radicals and iron.
  • the bridging group (A) can be represented by C 1 to C 6 alkylenes, substituted C 1 to C 6 alkylenes, oxygen, sulfur, R′ 2 C ⁇ , R′ 2 Si ⁇ , ⁇ Si(R′) 2 Si(R′ 2 ) ⁇ , R′ 2 Ge ⁇ , and R′P ⁇ , where “ ⁇ ” represents two chemical bonds, R′ is independently selected from the group consisting of hydride, hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, hydrocarbyl-substituted organometalloid, halocarbyl-substituted organometalloid, disubstituted boron, disubstituted Group 15 atoms, substituted Group 16 atoms, and halogen radical; and where two or more R′
  • the bridged metallocene catalyst compound of formula (II) includes two or more bridging groups (A).
  • (A) can be a divalent bridging group bound to both Cp A and Cp B selected from the group consisting of divalent C 1 to C 20 hydrocarbyls and C 1 to C 20 heteroatom containing hydrocarbonyls, where the heteroatom containing hydrocarbonyls include from one to three heteroatoms.
  • the bridging group (A) can include methylene, ethylene, ethylidene, propylidene, isopropylidene, diphenylmethylene, 1,2-dimethylethylene, 1,2-diphenylethylene, 1,1,2,2-tetramethylethylene, dimethylsilyl, diethylsilyl, methyl-ethylsilyl, trifluoromethylbutylsilyl, bis(trifluoromethyl)silyl, di(n-butyl)silyl, di(n-propyl)silyl, di(i-propyl)silyl, di(n-hexyl)silyl, dicyclohexylsilyl, diphenylsilyl, cyclohexylphenylsilyl, t-butylcyclohexylsilyl, di(t-butylphenyl)silyl, di(p-tolyl)silyl,and the corresponding moieties where the
  • the bridging group (A) can also include —Si(hydrocarbyl)2-O-(hydrocarbyl)2Si—Si(substitutedhydrocarbyl)2-O-(substitutedhydrocarbyl)2Si— groups and the like such as —SiMe2-O—SiMe2- and —SiPh2-O—SiPh2-.
  • the bridging group (A) can also be cyclic, having, for example, 4 to 10 ring members; in a more particular exemplary embodiment, bridging group (A) can have 5 to 7 ring members.
  • the ring members can be selected from the elements mentioned above, and, in a particular embodiment, can be selected from one or more of B, C, Si, Ge, N, and O.
  • Non-limiting examples of ring structures which can be present as, or as part of, the bridging moiety are cyclobutylidene, cyclopentylidene, cyclohexylidene, cycloheptylidene, cyclooctylidene and the corresponding rings where one or two carbon atoms are replaced by at least one of Si, Ge, N and O. In one or more embodiments, one or two carbon atoms can be replaced by at least one of Si and Ge.
  • the bonding arrangement between the ring and the Cp groups can be cis-, trans-, or a combination thereof.
  • the cyclic bridging groups (A) can be saturated or unsaturated and/or can carry one or more substituents and/or can be fused to one or more other ring structures. If present, the one or more substituents can be, in at least one specific embodiment, selected from the group consisting of hydrocarbyl (e.g., alkyl, such as methyl) and halogen (e.g., F, Cl).
  • hydrocarbyl e.g., alkyl, such as methyl
  • halogen e.g., F, Cl
  • the one or more Cp groups to which the above cyclic bridging moieties can optionally be fused can be saturated or unsaturated, and are selected from the group consisting of those having 4 to 10, more particularly 5, 6, or 7 ring members (selected from the group consisting of C, N, O, and S in a particular exemplary embodiment) such as, for example, cyclopentyl, cyclohexyl and phenyl.
  • these ring structures can themselves be fused such as, for example, in the case of a naphthyl group.
  • these (optionally fused) ring structures can carry one or more substituents.
  • substituents are hydrocarbyl (particularly alkyl) groups and halogen atoms.
  • the ligands Cp A and Cp B of formula (I) and (II) can be different from each other.
  • the ligands Cp A and Cp B of formula (I) and (II) can be the same.
  • the metallocene catalyst compound can include bridged mono-ligand metallocene compounds (e.g., mono cyclopentadienyl catalyst components).
  • metallocene catalyst components discussed and described above include their structural or optical or enantiomeric isomers (racemic mixture), and, in one exemplary embodiment, can be a pure enantiomer.
  • a single, bridged, asymmetrically substituted metallocene catalyst compound having a racemic and/or meso isomer does not, itself, constitute at least two different bridged, metallocene catalyst components.
  • the amount of the transition metal component of the one or more metallocene catalyst compounds in the catalyst system can range from a low of about 0.0.01 wt. %, about 0.2 wt %, about 3 wt. %, about 0.5 wt. %, or about 0.7 wt. % to a high of about 1 wt. %, about 2 wt. %, about 2.5 wt. %, about 3 wt. %, about 3.5 wt. %, or about 4 wt. %, based on the total weight of the catalyst system.
  • the “metallocene catalyst compound” can include any combination of any “embodiment” discussed and described herein.
  • the metallocene catalyst compound can include, but is not limited to, bis(n-propylcyclopentadienyl) hafnium (CH 3 ) 2 , bis(n-propylcyclopentadienyl) hafnium F 2 , bis(n-propylcyclopentadienyl) hafnium Cl 2 , or bis(n-butyl, methyl cyclopentadienyl) zirconium Cl 2 , or any combination thereof.
  • sCGC supported constrained geometry catalysts
  • sCGC supported constrained geometry catalysts
  • the sCGC catalyst may include a borate ion.
  • the borate anion is represented by the formula [BQ 4-z′ (G q (T-H) r ) z′ ] d ⁇ , wherein: B is boron in a valence state of 3; Q is selected from the group consisting of hydride, dihydrocarbylamido, halide, hydrocarbyloxide, hydrocarbyl, and substituted-hydrocarbyl radicals; z′ is an integer in a range from 1 to 4; G is a polyvalent hydrocarbon radical having r+1 valencies bonded to M′ and r groups (T-H); q is an integer, 0 or 1; the group (T-H) is a radical wherein T includes O, S, NR, or PR, the O, S, N or P atom of which is bonded to hydrogen atom H, wherein R is a hydrocarbyl radical, a trihydrocarbylsilyl radical, a trihydrocarbyl germyl radical or hydrogen; r is an integer
  • the borate ion may be representative by the formula [BQ 4-z′ (G q (T-M°R C x-1 X a y ) r ) z′ ] d ⁇ , wherein: B is boron in a valence state of 3; Q is selected from the group consisting of hydride, dihydrocarbylamido, halide, hydrocarbyloxide, hydrocarbyl, and substituted-hydrocarbyl radicals; z′ is an integer in a range from 1 to 4; G is a polyvalent hydrocarbon radical having r+1 valencies bonded to B and r groups (T-M°R C x-1 X a y ); q is an integer, 0 or 1; the group (T-M°R C x-1 X a y ) is a radical wherein T includes O, S, NR, or PR, the O, S, N or P atom of which is bonded to M°, wherein R is a
  • the catalyst system can include other single site catalysts such as Group 15-containing catalysts.
  • the catalyst system can include one or more second catalysts in addition to the single site catalyst compound such as chromium-based catalysts, Ziegler-Natta catalysts, one or more additional single-site catalysts such as metallocenes or Group 15-containing catalysts, bimetallic catalysts, and mixed catalysts.
  • the catalyst system can also include AlCl 3 , cobalt, iron, palladium, or any combination thereof.
  • MCN compounds examples include the hafnium compound shown as formula (III), the zirconium compounds shown as formulas (IV-A-C), and bridged zirconium compounds, shown as formulas (V-A-B).
  • each of these substituents may independently be a methyl group (Me), a chloro group (Cl), a fluoro group (F), or any number of other groups, including organic groups, or heteroatom groups. Further, these substituents will change during the reaction, as a pre-catalyst is converted to the active catalyst for the reaction. Further, any number of other substituents may be used on the ring structures, including any of the substituents described above with respect to formulas (I) and (II).
  • the catalyst system can include one or more Group 15 metal-containing catalyst compounds.
  • the Group 15 metal-containing compound generally includes a Group 3 to 14 metal atom, a Group 3 to 7, or a Group 4 to 6 metal atom.
  • the Group 15 metal-containing compound includes a Group 4 metal atom bound to at least one leaving group and also bound to at least two Group 15 atoms, at least one of which is also bound to a Group 15 or 16 atom through another group.
  • At least one of the Group 15 atoms is also bound to a Group 15 or 16 atom through another group which may be a C 1 to C 20 hydrocarbon group, a heteroatom containing group, silicon, germanium, tin, lead, or phosphorus, wherein the Group 15 or 16 atom may also be bound to nothing or a hydrogen, a Group 14 atom containing group, a halogen, or a heteroatom containing group, and wherein each of the two Group 15 atoms are also bound to a cyclic group and can optionally be bound to hydrogen, a halogen, a heteroatom or a hydrocarbyl group, or a heteroatom containing group.
  • the Group 15-containing metal compounds can be described more particularly with formulas (VI) or (VII):
  • M is a Group 3 to 12 transition metal or a Group 13 or 14 main group metal, a Group 4, 5, or 6 metal.
  • M is a Group 4 metal, such as zirconium, titanium or hafnium.
  • Each X is independently a leaving group, such as an anionic leaving group.
  • the leaving group may include a hydrogen, a hydrocarbyl group, a heteroatom, a halogen, or an alkyl; y is 0 or 1 (when y is 0 group L′ is absent).
  • the term ‘n’ is the oxidation state of M. In various embodiments, n is +3, +4, or +5. In many embodiments, n is +4.
  • m represents the formal charge of the YZL or the YZL′ ligand, and is 0, ⁇ 1, ⁇ 2 or ⁇ 3 in various embodiments. In many embodiments, m is ⁇ 2.
  • L is a Group 15 or 16 element, such as nitrogen; L′ is a Group 15 or 16 element or Group 14 containing group, such as carbon, silicon or germanium.
  • Y is a Group 15 element, such as nitrogen or phosphorus. In many embodiments, Y is nitrogen.
  • Z is a Group 15 element, such as nitrogen or phosphorus. In many embodiments, Z is nitrogen.
  • R 1 and R 2 are, independently, a C 1 to C 20 hydrocarbon group, a heteroatom containing group having up to twenty carbon atoms, silicon, germanium, tin, lead, or phosphorus.
  • R 1 and R 2 are a C 2 to C 20 alkyl, aryl, or aralkyl group, such as a linear, branched, or cyclic C 2 to C 20 alkyl group, or a C 2 to C 6 hydrocarbon group.
  • R 1 and R 2 may also be interconnected to each other.
  • R 3 may be absent or may be a hydrocarbon group, a hydrogen, a halogen, a heteroatom containing group.
  • R 3 is absent or a hydrogen, or a linear, cyclic or branched alkyl group having 1 to 20 carbon atoms.
  • R 4 and R 5 are independently an alkyl group, an aryl group, substituted aryl group, a cyclic alkyl group, a substituted cyclic alkyl group, a cyclic aralkyl group, a substituted cyclic aralkyl group or multiple ring system, often having up to 20 carbon atoms.
  • R 4 and R 5 have between 3 and 10 carbon atoms, or are a C 1 to C 20 hydrocarbon group, a C 1 to C 20 aryl group or a C 1 to C 20 aralkyl group, or a heteroatom containing group.
  • R 4 and R 5 may be interconnected to each other.
  • R 6 and R 7 are independently absent, hydrogen, an alkyl group, halogen, heteroatom, or a hydrocarbyl group, such as a linear, cyclic, or branched alkyl group having 1 to 20 carbon atoms.
  • R 6 and R 7 are absent.
  • R. may be absent, or may be a hydrogen, a Group 14 atom containing group, a halogen, or a heteroatom containing group.
  • R 1 and R 2 may also be interconnected” it is meant that R 1 and R 2 may be directly bound to each other or may be bound to each other through other groups.
  • R 4 and R 5 may also be interconnected” it is meant that R 4 and R 5 may be directly bound to each other or may be bound to each other through other groups.
  • An alkyl group may be linear, branched alkyl radicals, alkenyl radicals, alkynyl radicals, cycloalkyl radicals, aryl radicals, acyl radicals, aroyl radicals, alkoxy radicals, aryloxy radicals, alkylthio radicals, dialkylamino radicals, alkoxycarbonyl radicals, aryloxycarbonyl radicals, carbomoyl radicals, alkyl- or dialkyl-carbamoyl radicals, acyloxy radicals, acylamino radicals, aroylamino radicals, straight, branched or cyclic, alkylene radicals, or combination thereof.
  • An aralkyl group is defined to be a substituted aryl group.
  • R 4 and R 5 are independently a group represented by the following formula (VIII).
  • R 8 to R 12 are each independently hydrogen, a C 1 to C 40 alkyl group, a halide, a heteroatom, a heteroatom containing group containing up to 40 carbon atoms.
  • R 8 to R 12 are a C 1 to C 20 linear or branched alkyl group, such as a methyl, ethyl, propyl, or butyl group. Any two of the R groups may form a cyclic group and/or a heterocyclic group.
  • the cyclic groups may be aromatic.
  • R 9 , R 10 and R 12 are independently a methyl, ethyl, propyl, or butyl group (including all isomers).
  • R 9 , R 10 and R 12 are methyl groups, and R 8 and R 11 are hydrogen.
  • R 4 and R 5 are both a group represented by the following formula (IX).
  • M is a Group 4 metal, such as zirconium, titanium, or hafnium. In many embodiments, M is zirconium.
  • Each of L, Y, and Z may be a nitrogen.
  • Each of R 1 and R 2 may be —CH 2 —CH 2 —.
  • R 3 may be hydrogen, and R 6 and R 7 may be absent.
  • the Group 15 metal-containing catalyst compound can be represented by the following formula (X).
  • Ph represents phenyl
  • the catalyst system may include a catalyst or catalyst component in a slurry, which may have an initial catalyst compound, and an added solution catalyst component that is added to the slurry.
  • the initial catalyst component slurry may have no catalysts. In this case, two or more solution catalysts may be added to the slurry to cause each to be supported.
  • the catalyst component slurry can include an activator and a support, or a supported activator.
  • the slurry can include a catalyst compound in addition to the activator and the support.
  • the catalyst compound in the slurry may be supported.
  • the slurry may include one or more activators and supports, and one more catalyst compounds.
  • the slurry may include two or more activators (such as alumoxane and a modified alumoxane) and a catalyst compound, or the slurry may include a supported activator and more than one catalyst compounds.
  • the slurry includes a support, an activator, and two catalyst compounds.
  • the slurry includes a support, an activator and two different catalyst compounds, which may be added to the slurry separately or in combination.
  • the slurry, containing silica and alumoxane may be contacted with a catalyst compound, allowed to react, and thereafter the slurry is contacted with another catalyst compound, for example, in a trim system.
  • the molar ratio of metal in the activator to metal in the pre-catalyst compound in the slurry may be 1000:1 to 0.5:1, 300:1 to 1:1, or 150:1 to 1:1.
  • the slurry can include a support material which may be any inert particulate carrier material known in the art, including, but not limited to, silica, fumed silica, alumina, clay, talc or other support materials such as disclosed above.
  • the slurry contains silica and an activator, such as methyl aluminoxane (“MAO”), modified methyl aluminoxane (“MMAO”), as discussed further below.
  • MAO methyl aluminoxane
  • MMAO modified methyl aluminoxane
  • One or more diluents or carriers can be used to facilitate the combination of any two or more components of the catalyst system in the slurry or in the trim catalyst solution.
  • the single site catalyst compound and the activator can be combined together in the presence of toluene or another non-reactive hydrocarbon or hydrocarbon mixture to provide the catalyst mixture.
  • other suitable diluents can include, but are not limited to, ethylbenzene, xylene, pentane, hexane, heptane, octane, other hydrocarbons, or any combination thereof.
  • the support either dry or mixed with toluene can then be added to the catalyst mixture or the catalyst/activator mixture can be added to the support.
  • the terms “support” and “carrier” are used interchangeably and refer to any support material, including a porous support material, such as talc, inorganic oxides, and inorganic chlorides.
  • the one or more single site catalyst compounds of the slurry can be supported on the same or separate supports together with the activator, or the activator can be used in an unsupported form, or can be deposited on a support different from the single site catalyst compounds, or any combination thereof. This may be accomplished by any technique commonly used in the art.
  • the single site catalyst compound can contain a polymer bound ligand.
  • the single site catalyst compounds of the slurry can be spray dried.
  • the support used with the single site catalyst compound can be functionalized.
  • the support can be or include one or more inorganic oxides, for example, of Group 2, 3, 4, 5, 13, or 14 elements.
  • the inorganic oxide can include, but is not limited to silica, alumina, titania, zirconia, boria, zinc oxide, magnesia, or any combination thereof.
  • Illustrative combinations of inorganic oxides can include, but are not limited to, alumina-silica, silica-titania, alumina-silica-titania, alumina-zirconia, alumina-titania, and the like.
  • the support can be or include alumina, silica, or a combination thereof. In one embodiment described herein, the support is silica.
  • Suitable commercially available silica supports can include, but are not limited to, ES757, ES70, and ES70W available from PQ Corporation.
  • Suitable commercially available silica-alumina supports can include, but are not limited to, SIRAL® 1, SIRAL® 5, SIRAL® 10, SIRAL® 20, SIRAL® 28M, SIRAL® 30, and SIRAL® 40, available from SASOL®.
  • catalyst supports comprising silica gels with activators, such as methylaluminoxanes (MAOs), are used in the trim systems described, since these supports may function better for co-supporting solution carried catalysts.
  • Suitable supports may also be selected from the Cab-o-sil® materials available from Cabot Corporation and silica materials available from the Grace division of W.R. Grace & Company.
  • Catalyst supports may also include polymers that are covalently bonded to a ligand on the catalyst.
  • polymers that are covalently bonded to a ligand on the catalyst.
  • two or more catalyst molecules may be bonded to a single polyolefin chain.
  • the term “activator” may refer to any compound or combination of compounds, supported, or unsupported, which can activate a single site catalyst compound or component, such as by creating a cationic species of the catalyst component. For example, this can include the abstraction of at least one leaving group (the “X” group in the single site catalyst compounds described herein) from the metal center of the single site catalyst compound/component.
  • the activator may also be referred to as a “co-catalyst”.
  • the activator can include a Lewis acid or a non-coordinating ionic activator or ionizing activator, or any other compound including Lewis bases, aluminum alkyls, and/or conventional-type co-catalysts.
  • illustrative activators can include, but are not limited to, aluminoxane or modified aluminoxane, and/or ionizing compounds, neutral or ionic, such as Dimethylanilinium tetrakis(pentafluorophenyl)borate, Triphenylcarbenium tetrakis(pentafluorophenyl)borate, Dimethylanilinium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Triphenylcarbenium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Diphenylcarbenium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Diphen
  • activators may or may not bind directly to the support surface or may be modified to allow them to be bound to a support surface while still maintaining their compatability with the polymerization system.
  • tethering agents may be derived from groups that are reactive with surface hydroxyl species.
  • reactive functional groups include aluminum halides, aluminum hydrides, aluminum alkyls, aluminum aryls, aluminum alkoxides, electrophilic silicon reagents, alkoxy silanes, amino silanes, boranes.
  • Aluminoxanes can be described as oligomeric aluminum compounds having —Al(R)—O— subunits, where R is an alkyl group.
  • aluminoxanes include, but are not limited to, methylaluminoxane (“MAO”), modified methylaluminoxane (“MMAO”), ethylaluminoxane, isobutylaluminoxane, or a combination thereof.
  • Aluminoxanes can be produced by the hydrolysis of the respective trialkylaluminum compound.
  • MMAO can be produced by the hydrolysis of trimethylaluminum and a higher trialkylaluminum, such as triisobutylaluminum.
  • MMAOs are generally more soluble in aliphatic solvents and more stable during storage. There are a variety of methods for preparing aluminoxane and modified aluminoxanes.
  • a visually clear MAO can be used.
  • a cloudy or gelled aluminoxane can be filtered to produce a clear aluminoxane or clear aluminoxane can be decanted from a cloudy aluminoxane solution.
  • a cloudy and/or gelled aluminoxane can be used.
  • Another aluminoxane can include a modified methyl aluminoxane (“MMAO”) type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylaluminoxane type 3A, discussed and described in U.S. Pat. No. 5,041,584).
  • MMAO modified methyl aluminoxane
  • a suitable source of MAO can be a solution having from about 1 wt. % to about a 50 wt. % MAO, for example.
  • Commercially available MAO solutions can include the 10 wt. % and 30 wt. % MAO solutions available from Albemarle Corporation, of Baton Rouge, La.
  • one or more organo-aluminum compounds such as one or more alkylaluminum compounds can be used in conjunction with the aluminoxanes.
  • alkylaluminum species that may be used are diethylaluminum ethoxide, diethylaluminum chloride, and/or diisobutylaluminum hydride.
  • trialkylaluminum compounds include, but are not limited to, trimethylaluminum, triethylaluminum (“TEAL”), triisobutylaluminum (“TiBAl”), tri-n-hexylaluminum, tri-n-octylaluminum, tripropylaluminum, tributylaluminum, and the like.
  • the catalyst component solution may include only a catalyst compound or may include an activator in addition to the catalyst compound.
  • the catalyst solution used in the trim process can be prepared by dissolving the catalyst compound and optional activators in a liquid solvent.
  • the liquid solvent may be an alkane, such as a C 5 to C 30 alkane, or a C 5 to C 10 alkane. Cyclic alkanes such as cyclohexane and aromatic compounds such as toluene may also be used.
  • mineral oil may be used as a solvent.
  • the solution employed should be liquid under the conditions of polymerization and relatively inert.
  • the liquid utilized in the catalyst compound solution is different from the diluent used in the catalyst component slurry.
  • the liquid utilized in the catalyst compound solution is the same as the diluent used in the catalyst component solution.
  • the ratio of metal in the activator to metal in the pre-catalyst compound in the solution may be 1000:1 to 0.5:1, 300:1 to 1:1, or 150:1 to 1:1. In certain cases, it may be advantageous to have an excess of catalyst compound such that the ratio is ⁇ 1:1, for example, 1:1 to 0.5:1 or 1:1 to 0.1:1 or 1:1 to 0.01.
  • the activator and catalyst compound is present in the solution at up to about 90 wt. %, at up to about 50 wt. %, at up to about 20 wt. %, preferably at up to about 10 wt. %, at up to about 5 wt. %, at less than 1 wt. %, or between 100 ppm and 1 wt. %, based upon the weight of the solvent and the activator or catalyst compound.
  • the catalyst component solution can comprise any one of the soluble catalyst compounds described in the catalyst section herein. As the catalyst is dissolved in the solution, a higher solubility is desirable. Accordingly, the catalyst compound in the catalyst component solution may often include a metallocene, which may have higher solubility than other catalysts.
  • any of the above described catalyst component containing solutions may be combined with any of the catalyst component containing slurry/slurries described above.
  • more than one catalyst component solution may be utilized.
  • a static control agent is a chemical composition which, when introduced into a fluidized bed reactor, may influence or drive the static charge (negatively, positively, or to zero) in the fluidized bed.
  • the specific static control agent used may depend upon the nature of the static charge, and the choice of static control agent may vary dependent upon the polymer being produced and the single site catalyst compounds being used.
  • Control agents such as aluminum stearate may be employed.
  • the static control agent used may be selected for its ability to receive the static charge in the fluidized bed without adversely affecting productivity.
  • Other suitable static control agents may also include aluminum distearate, ethoxlated amines, and anti-static compositions such as those provided by Innospec Inc. under the trade name OCTASTAT.
  • OCTASTAT 2000 is a mixture of a polysulfone copolymer, a polymeric polyamine, and oil-soluble sulfonic acid.
  • control agents any of the aforementioned control agents, as well as those described in, for example, WO 01/44322, listed under the heading Carboxylate Metal Salt and including those chemicals and compositions listed as antistatic agents may be employed either alone or in combination as a control agent.
  • the carboxylate metal salt may be combined with an amine containing control agent (e.g., a carboxylate metal salt with any family member belonging to the KEMAMINE® (available from Crompton Corporation) or ATMER® (available from ICI Americas Inc.) family of products).
  • an amine containing control agent e.g., a carboxylate metal salt with any family member belonging to the KEMAMINE® (available from Crompton Corporation) or ATMER® (available from ICI Americas Inc.) family of products).
  • the polyethyleneimines may be linear, branched, or hyperbranched (e.g., forming dendritic or arborescent polymer structures). They can be a homopolymer or copolymer of ethyleneimine or mixtures thereof (referred to as polyethyleneimine(s) hereafter). Although linear polymers represented by the chemical formula —[CH 2 —CH 2 —NH]— may be used as the polyethyleneimine, materials having primary, secondary, and tertiary branches can also be used. Commercial polyethyleneimine can be a compound having branches of the ethyleneimine polymer. Suitable polyethyleneimines are commercially available from BASF Corporation under the trade name Lupasol.
  • Another useful continuity additive can include a mixture of aluminum distearate and an ethoxylated amine-type compound, e.g., IRGASTAT AS-990, available from Huntsman (formerly Ciba Specialty Chemicals).
  • the mixture of aluminum distearate and ethoxylated amine type compound can be slurried in mineral oil e.g., Hydrobrite 380.
  • the mixture of aluminum distearate and an ethoxylated amine type compound can be slurried in mineral oil to have total slurry concentration of ranging from about 5 wt. % to about 50 wt. % or about 10 wt. % to about 40 wt. %, or about 15 wt. % to about 30 wt. %.
  • the continuity additive(s) or static control agent(s) may be added to the reactor in an amount ranging from 0.05 to 200 ppm, based on the weight of all feeds to the reactor, excluding recycle. In some embodiments, the continuity additive may be added in an amount ranging from 2 to 100 ppm, or in an amount ranging from 4 to 50 ppm.
  • FIG. 1 is a schematic of a gas-phase reactor system 100 , showing the addition of at least two catalysts, at least one of which is added as a trim catalyst.
  • the catalyst component slurry preferably a mineral oil slurry including at least one support and at least one activator, at least one supported activator, and optional catalyst compounds may be placed in a vessel or catalyst pot (cat pot) 102 .
  • the cat pot 102 is an agitated holding tank designed to keep the solids concentration homogenous.
  • a catalyst component solution, prepared by mixing a solvent and at least one catalyst compound and/or activator, is placed in another vessel, which can be termed a trim pot 104 .
  • the catalyst component slurry can then be combined in-line with the catalyst component solution to form a final catalyst composition.
  • a nucleating agent 106 such as silica, alumina, fumed silica or any other particulate matter may be added to the slurry and/or the solution in-line or in the vessels 102 or 104 .
  • additional activators or catalyst compounds may be added in-line.
  • a second catalyst slurry that includes a different catalyst may be introduced from a second cat pot. The two catalyst slurries may be used as the catalyst system with or without the addition of a solution catalyst from the trim pot.
  • the catalyst component slurry and solution can be mixed in-line.
  • the solution and slurry may be mixed by utilizing a static mixer 108 or an agitating vessel (not shown).
  • the mixing of the catalyst component slurry and the catalyst component solution should be long enough to allow the catalyst compound in the catalyst component solution to disperse in the catalyst component slurry such that the catalyst component, originally in the solution, migrates to the supported activator originally present in the slurry.
  • the combination forms a uniform dispersion of catalyst compounds on the supported activator forming the catalyst composition.
  • the length of time that the slurry and the solution are contacted is typically up to about 120 minutes, such as about 0.01 to about 60 minutes, about 5 to about 40 minutes, or about 10 to about 30 minutes.
  • the combination yield a new polymerization catalyst in less than 1 h, less than 30 min, or less than 15 min. Shorter times are more effective, as the new catalyst is ready before being introduces into the reactor, providing the potential for faster flow rates.
  • an aluminum alkyl, an ethoxylated aluminum alkyl, an aluminoxane, an anti-static agent or a borate activator such as a C 1 to C 15 alkyl aluminum (for example tri-isobutyl aluminum, trimethyl aluminum or the like), a C 1 to C 15 ethoxylated alkyl aluminum or methyl aluminoxane, ethyl aluminoxane, isobutylaluminoxane, modified aluminoxane or the like are added to the mixture of the slurry and the solution in line.
  • the alkyls, antistatic agents, borate activators and/or aluminoxanes may be added from an alkyl vessel 110 directly to the combination of the solution and the slurry, or may be added via an additional alkane (such as isopentane, hexane, heptane, and or octane) carrier stream, for example, from a hydrocarbon vessel 112 .
  • the additional alkyls, antistatic agents, borate activators and/or aluminoxanes may be present at up to about 500 ppm, at about 1 to about 300 ppm, at 10 to about 300 ppm, or at about 10 to about 100 ppm.
  • Carrier streams that may be used include isopentane and or hexane, among others.
  • the carrier may be added to the mixture of the slurry and the solution, typically at a rate of about 0.5 to about 60 lbs/hr (27 kg/hr) or greater, depending on reactor size.
  • a carrier gas 114 such as nitrogen, argon, ethane, propane and the like, may be added in-line to the mixture of the slurry and the solution.
  • the carrier gas may be added at the rate of about 1 to about 100 lb/hr (0.4 to 45 kg/hr), or about 1 to about 50 lb/hr (5 to 23 kg/hr), or about 1 to about 25 lb/hr (0.4 to 11 kg/hr).
  • a liquid carrier stream is introduced into the combination of the solution and slurry that is moving in a downward direction.
  • the mixture of the solution, the slurry and the liquid carrier stream may pass through a mixer or length of tube for mixing before being contacted with a gaseous carrier stream.
  • a comonomer 116 such as hexene, another alpha-olefin or diolefin, may be added in-line to the mixture of the slurry and the solution.
  • the slurry/solution mixture is then passed through an injection tube 118 to a reactor 120 .
  • a nucleating agent 122 such as fumed silica, can be added directly into the reactor 120 .
  • the injection tube may aerosolize the slurry/solution mixture. Any number of suitable tubing sizes and configurations may be used to aerosolize and/or inject the slurry/solution mixture.
  • a gas stream 124 such as cycle gas, or re-cycle gas 126 , monomer, nitrogen, or other materials is introduced into a support tube 128 that surrounds the injection tube 118 .
  • oxygen or fluorobenzene can be added to the reactor 120 directly or to the gas stream 124 to control the polymerization rate.
  • a metallocene catalyst which is sensitive to oxygen or fluorobenzene
  • oxygen can be used to modify the metallocene polymerization rate relative to the polymerization rate of the other catalyst.
  • An example of such a catalyst combination is bis(n-propyl cyclopentadienyl)zirconium dichloride and [(2,4,6-Me 3 C 6 H 2 )NCH 2 CH 2 ] 2 NHZrBn 2 , where Me is methyl, or bis(indenyl)zirconium dichloride and [(2,4,6-Me 3 C 6 H 2 )NCH 2 CH 2 ] 2 NHHfBn 2 , where Me is methyl.
  • the contact temperature of the slurry and the solution is in the range of from 0° C. to about 80° C., from about 0° C. to about 60° C., from about 10° C., to about 50° C. and from about 20° C. to about 40° C.
  • a slurry can be combined with two or more solutions having the same or different catalyst compounds and or activators.
  • the solution may be combined with two or more slurries each having the same or different supports, and the same or different catalyst compounds and or activators.
  • two or more slurries combined with two or more solutions, preferably in-line where the slurries each comprise the same or different supports and may comprise the same or different catalyst compounds and or activators and the solutions comprise the same or different catalyst compounds and or activators.
  • the slurry may contain a supported activator and two different catalyst compounds, and two solutions, each containing one of the catalysts in the slurry, are each independently combined, in-line, with the slurry.
  • the properties of the product polymer may be controlled by adjusting the timing, temperature, concentrations, and sequence of the mixing of the solution, the slurry and any optional added materials (nucleating agents, catalyst compounds, activators, etc) described above.
  • the MWD, composition distribution, melt index, relative amount of polymer produced by each catalyst, and other properties of the polymer produced may also be changed by manipulating process parameters. Any number of process parameters may be adjusted, including manipulating hydrogen concentration in the polymerization system, changing the amount of the first catalyst in the polymerization system, changing the amount of the second catalyst in the polymerization system. Other process parameters that can be adjusted include changing the relative ratio of the catalyst in the polymerization process (and optionally adjusting their individual feed rates to maintain a steady or constant resin production rate).
  • the concentrations of reactants in the reactor 120 can be adjusted by changing the amount of liquid or gas that is withdrawn or purged from the process, changing the amount and/or composition of a recovered liquid and/or recovered gas returned to the polymerization process, wherein the recovered liquid or recovered gas can be recovered from polymer discharged from the polymerization process.
  • Further concentration parameters that can be adjusted include changing the polymerization temperature, changing the ethylene partial pressure in the polymerization process, changing the ethylene to comonomer ratio in the polymerization process, changing the activator to transition metal ratio in the activation sequence.
  • Time dependant parameters may be adjusted, such as changing the relative feed rates of the slurry or solution, changing the mixing time, the temperature and or degree of mixing of the slurry and the solution in-line, adding different types of activator compounds to the polymerization process, and adding oxygen or fluorobenzene or other catalyst poison to the polymerization process. Any combinations of these adjustments may be used to control the properties of the final polymer product.
  • the composition distribution of the polymer product is measured at regular intervals and one of the above process parameters, such as temperature, catalyst compound feed rate, the ratio of the two or more catalysts to each other, the ratio of comonomer to monomer, the monomer partial pressure, and or hydrogen concentration, is altered to bring the composition to the desired level, if necessary.
  • the composition distribution may be performed by temperature rising elution fractionation (TREF), or similar techniques TREF measures composition as a function of elution temperature.
  • a polymer product property is measured in-line and in response the ratio of the catalysts being combined is altered.
  • the molar ratio of the catalyst compound in the catalyst component slurry to the catalyst compound in the catalyst component solution, after the slurry and solution have been mixed to form the final catalyst composition is 500:1 to 1:500, or 100:1 to 1:100, or 50:1 to 1:50, or 10:1 to 1:10, or 5:1 to 1:5.
  • the molar ratio of a Group 15 catalyst compound in the slurry to a ligand metallocene catalyst compound in the solution, after the slurry and solution have been mixed to form the catalyst composition is 500:1, 100:1, 50:1, 10:1, 5:1, 1:5, 1:10, 1:100, or 1:500.
  • the product property measured can include the polymer product's flow index, melt index, density, MWD, comonomer content, composition distribution, and combinations thereof.
  • the ratio of the catalyst compounds is altered, the introduction rate of the catalyst composition to the reactor, or other process parameters, is altered to maintain a desired production rate.
  • the processes described herein immobilize the solution catalyst compound in and on a support, preferably a supported activator.
  • the in-line immobilization techniques described herein preferably result in a supported catalyst system that when introduced to the reactor provides for suitable polymer properties, with appropriate particle morphology, bulk density, or higher catalyst activities and without the need for additional equipment in order to introduce catalyst compound solution into a reactor, particularly a gas phase or slurry phase reactor.
  • the catalyst system can be used to polymerize one or more olefins to provide one or more polymer products therefrom.
  • Any suitable polymerization process can be used, including, but not limited to, high pressure, solution, slurry, and/or gas phase polymerization processes.
  • modifications to a catalyst addition system that are similar to those discussed with respect to FIG. 1 can be used.
  • a trim system may be used to feed catalyst to a loop slurry reactor for polyethylene copolymer production.
  • polyethylene and “polyethylene copolymer” refer to a polymer having at least 50 wt. % ethylene-derived units.
  • the polyethylene can have at least 70 wt. % ethylene-derived units, at least 80 wt. % ethylene-derived units, at least 90 wt. % ethylene-derived units, at least 95 wt. % ethylene-derived units, or 100 wt. % ethylene-derived units.
  • the polyethylene can, thus, be a homopolymer or a copolymer, including a terpolymer, having one or more other monomeric units.
  • a polyethylene can include, for example, at least one or more other olefins or comonomers.
  • Suitable comonomers can contain 3 to 16 carbon atoms, from 3 to 12 carbon atoms, from 4 to 10 carbon atoms, and from 4 to 8 carbon atoms.
  • Examples of comonomers include, but are not limited to, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 4-methylpent-1-ene, 1-decene, 1-dodecene, 1-hexadecene, and the like.
  • small amounts of diene monomers, such as 1,7-octadiene may be added to the polymerization to adjust polymer properties.
  • the fluidized bed reactor 120 can include a reaction zone 130 and a velocity reduction zone 132 .
  • the reaction zone 130 can include a bed 134 that includes growing polymer particles, formed polymer particles and a minor amount of catalyst particles fluidized by the continuous flow of the gaseous monomer and diluent to remove heat of polymerization through the reaction zone.
  • some of the re-circulated gases 124 can be cooled and compressed to form liquids that increase the heat removal capacity of the circulating gas stream when readmitted to the reaction zone.
  • a suitable rate of gas flow can be readily determined by experimentation.
  • Make-up of gaseous monomer to the circulating gas stream can be at a rate equal to the rate at which particulate polymer product and monomer associated therewith is withdrawn from the reactor and the composition of the gas passing through the reactor can be adjusted to maintain an essentially steady state gaseous composition within the reaction zone.
  • the gas leaving the reaction zone 130 can be passed to the velocity reduction zone 132 where entrained particles are removed, for example, by slowing and falling back to the reaction zone 130 . If desired, finer entrained particles and dust can be removed in a separation system 136 , such as a cyclone and/or fines filter.
  • the gas 124 can be passed through a heat exchanger 138 where at least a portion of the heat of polymerization can be removed. The gas can then be compressed in a compressor 140 and returned to the reaction zone 130 .
  • the reactor temperature of the fluid bed process can be greater than about 30° C., about 40° C., about 50° C., about 90° C., about 100° C., about 110° C., about 120° C., about 150° C., or higher.
  • the reactor temperature is operated at the highest feasible temperature taking into account the sintering temperature of the polymer product within the reactor.
  • Preferred reactor temperatures are between 70 and 95° C. More preferred reactor temperatures are between 75 and 90° C.
  • the upper temperature limit in one embodiment is the melting temperature of the polyethylene copolymer produced in the reactor.
  • higher temperatures may result in narrower MWDs, which can be improved by the addition of the MCN, or other, co-catalysts, as described herein.
  • Hydrogen gas can be used in olefin polymerization to control the final properties of the polyolefin.
  • increasing concentrations (partial pressures) of hydrogen can increase the flow index (FI) of the polyethylene copolymer generated.
  • the flow index can thus be influenced by the hydrogen concentration.
  • the amount of hydrogen in the polymerization can be expressed as a mole ratio relative to the total polymerizable monomer, for example, ethylene, or a blend of ethylene and hexene or propylene.
  • the amount of hydrogen used in the polymerization process can be an amount necessary to achieve the desired flow index of the final polyolefin resin.
  • the mole ratio of hydrogen to total monomer (H 2 :monomer) can be greater than about 0.0001, greater than about 0.0005, or greater than about 0.001.
  • the mole ratio of hydrogen to total monomer (H 2 :monomer) can be less than about 10, less than about 5, less than about 3, and less than about 0.10.
  • a desirable range for the mole ratio of hydrogen to monomer can include any combination of any upper mole ratio limit with any lower mole ratio limit described herein.
  • the amount of hydrogen in the reactor at any time can range to up to about 5,000 ppm, up to about 4,000 ppm in another embodiment, up to about 3,000 ppm, or between about 50 ppm and 5,000 ppm, or between about 50 ppm and 2,000 ppm in another embodiment.
  • the amount of hydrogen in the reactor can range from a low of about 1 ppm, about 50 ppm, or about 100 ppm to a high of about 400 ppm, about 800 ppm, about 1,000 ppm, about 1,500 ppm, or about 2,000 ppm.
  • the ratio of hydrogen to total monomer (H 2 :monomer) can be about 0.00001:1 to about 2:1, about 0.005:1 to about 1.5:1, or about 0.0001:1 to about 1:1.
  • the one or more reactor pressures in a gas phase process can vary from 690 kPa (100 psig) to 3,448 kPa (500 psig), in the range from 1,379 kPa (200 psig) to 2,759 kPa (400 psig), or in the range from 1,724 kPa (250 psig) to 2,414 kPa (350 psig).
  • the gas phase reactor can be capable of producing from about 10 kg of polymer per hour (25 lbs/hr) to about 90,900 kg/hr (200,000 lbs/hr), or greater, and greater than about 455 kg/hr (1,000 lbs/hr), greater than about 4,540 kg/hr (10,000 lbs/hr), greater than about 11,300 kg/hr (25,000 lbs/hr), greater than about 15,900 kg/hr (35,000 lbs/hr), and greater than about 22,700 kg/hr (50,000 lbs/hr), and from about 29,000 kg/hr (65,000 lbs/hr) to about 45,500 kg/hr (100,000 lbs/hr).
  • a slurry polymerization process can also be used in embodiments.
  • a slurry polymerization process generally uses pressures in the range of from about 101 kPa (1 atmosphere) to about 5,070 kPa (50 atmospheres) or greater, and temperatures in the range of from about 0° C. to about 120° C., and more particularly from about 30° C. to about 100° C.
  • a suspension of solid, particulate polymer can be formed in a liquid polymerization diluent medium to which ethylene, comonomers, and hydrogen along with catalyst can be added.
  • the suspension including diluent can be intermittently or continuously removed from the reactor where the volatile components are separated from the polymer and recycled, optionally after a distillation, to the reactor.
  • the liquid diluent employed in the polymerization medium can be an alkane having from 3 to 7 carbon atoms, such as, for example, a branched alkane.
  • the medium employed should be liquid under the conditions of polymerization and relatively inert. When a propane medium is used the process should be operated above the reaction diluent critical temperature and pressure. In one embodiment, a hexane, isopentane, or isobutane medium can be employed.
  • the slurry can be circulated in a continuous loop system.
  • the product polyethylene can have a melt index ratio (MIR or I 21 /I 2 ) ranging from about 5 to about 300, or from about 10 to less than about 150, or, in many embodiments, from about 15 to about 50.
  • Flow index (FI, HLMI, or I 21 can be measured in accordance with ASTM D1238 (190° C., 21.6 kg).
  • the melt index (MI, I 2 ) can be measured in accordance with ASTM D1238 (at 190° C., 2.16 kg weight).
  • Density can be determined in accordance with ASTM D-792. Density is expressed as grams per cubic centimeter (g/cm 3 ) unless otherwise noted.
  • the polyethylene can have a density ranging from a low of about 0.89 g/cm 3 , about 0.90 g/cm 3 , or about 0.91 g/cm 3 to a high of about 0.95 g/cm 3 , about 0.96 g/cm 3 , or about 0.97 g/cm 3 .
  • the polyethylene can have a bulk density, measured in accordance with ASTM D1895 method B, of from about 0.25 g/cm 3 to about 0.5 g/cm 3 .
  • the bulk density of the polyethylene can range from a low of about 0.30 g/cm 3 , about 0.32 g/cm 3 , or about 0.33 g/cm 3 to a high of about 0.40 g/cm 3 , about 0.44 g/cm 3 , or about 0.48 g/cm 3 .
  • the polyethylene can be suitable for such articles as films, fibers, nonwoven and/or woven fabrics, extruded articles, and/or molded articles.
  • films include blown or cast films formed by coextrusion or by lamination useful as shrink film, cling film, stretch film, sealing films, oriented films, snack packaging, heavy duty bags, grocery sacks, baked and frozen food packaging, medical packaging, industrial liners, membranes, etc. in food-contact and non-food contact applications, agricultural films and sheets.
  • fibers include melt spinning, solution spinning and melt blown fiber operations for use in woven or non-woven form to make filters, diaper fabrics, hygiene products, medical garments, geotextiles, etc.
  • extruded articles examples include tubing, medical tubing, wire and cable coatings, pipe, geomembranes, and pond liners.
  • molded articles include single and multi-layered constructions in the form of bottles, tanks, large hollow articles, rigid food containers and toys, etc.
  • SCB short chain branching
  • LCB long chain branching
  • shorter chains lowers the melt temperature of the polymer, and may enhance the processability.
  • SCB on shorter chains may force these chains out of crystallites and into amorphous regions, lowering the toughness of the resulting polymer product.
  • Hydrogen may be added to the polymer reactions to control molecular weight.
  • the hydrogen acts as chain termination agent, essentially replacing a monomer or comonomer molecule in the reaction. This stops the formation of a current polymer chain, and allows a new polymer chain to begin.
  • the catalysts A-J shown in Table 1 were prepared as discussed below. All the catalysts prepared were screened in a fluidized bed reactor equipped with devices for temperature control, catalyst feeding or injection equipment, gas chromatograph (GC) analyzer for monitoring and controlling monomer and comonomer gas feeds and equipment for polymer sampling and collecting.
  • the reactor consisted of a 6 inch (15.24 cm) diameter bed section increasing to 10 inches (25.4 cm) at the reactor top. Gas comes in through a perforated distributor plate allowing fluidization of the bed contents and polymer sample is discharged at the reactor top.
  • the comonomer in the example polymerizations herein is 1-hexene.
  • the polymerization parameters are outlined in the table 1 below and plotted in FIGS. 2 and 3 .
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity 1-2 ft/sec (0.3 to 0.6 m/sec).
  • the reactor was operated at a temperature of 175 F (79 C) and total pressure of 300 psig (2274 kPa gauge) including 35 mol % ethylene.
  • FIG. 2 is a plot 200 of a series of polymers that were prepared to test the relative abilities of a series of metallocene catalysts to prepare a resin having about a 1 melt index (MI) and a density (D) of about 0.92.
  • the polymerizations were performed in the continuous gas phase reactor (LGPR) described above.
  • the left axis 202 represents the gas-phase ratios of hydrogen to ethylene monomer (H 2 /C 2 ) used to achieve the target properties, in units of parts-per-million (mol) of H 2 per mol % C 2 (ppm/mol %).
  • the right axis 204 represents the comonomer to ethylene ratio (C 6 /C 2 ) used to achieve the target properties, in units of mol per mol.
  • Comparing C 6 /C 2 levels used to achieve the property targets indicate the relative abilities of the catalysts to incorporate comonomer. For example, comparing the C 6 /C 2 level 206 for (1-EtInd) 2 ZrCl 2 (B) to the C 6 /C 2 level 208 for (PrCp) 2 HfF 2 (I) gives a ratio of about 36/9 or about four. This indicates that for a given C 6 /C 2 gas ratio, a polymer prepared with (PrCp) 2 HfF 2 will have approximately four times the short chain branching (SCB) of a polymer prepared using (1-EtInd) 2 ZrCl 2 .
  • SCB short chain branching
  • This data is useful for controlling composition distributions of polymers made as in-situ blends using catalyst mixtures, for example, as co-supported catalysts on a single support.
  • the data is also useful for determining which catalysts should be combined to have a composition distribution containing both comonomer rich (low density) and comonomer poor (high density) components.
  • FIG. 3 is a plot 300 of the series of polymers of FIG. 2 , showing the melt index ratio (MIR) of the series of polymers made by different metallocene (MCN) catalysts.
  • MIR melt index ratio
  • MFR melt flow ratio
  • I 21 /I 2 interchangeably refer to the ratio of the flow index (“FI” or “I 21 ”) to the melt index (“MI” or “I 2 ”).
  • the MI (I 2 ) can be measured in accordance with ASTM D1238 (at 190° C., 2.16 kg weight).
  • the FI (I 21 ) can be measured in accordance with ASTM D1238 (at 190° C., 21.6 kg weight).
  • ASTM D1238 at 190° C., 2.16 kg weight
  • FI I 21
  • Like numbered items are as described with respect to FIG. 2 .
  • the left axis 302 represents the MIR.
  • the MIR (which may also be termed melt flow ratio or MFR) is the ratio of the I21 and I2 melt indices and may indicate the presence of long chain branching. For linear resins, without LCB, the ratio is around 25 or less. Higher MIR values may indicate the presence of LCB which can be detrimental to film properties, as noted above.
  • the highest MIR ratio 304 was for (CH 2 ) 3 Si(CpMe 4 )CpZrCl 2 (J), indicating that polymer produced by this catalyst has the most LCB. In contrast, blending resins for with the two different catalysts forms a final product that will have a higher MIR.
  • catalysts were selected to determine the dependence of the molecular weight (Mw) on the H 2 ratio.
  • These catalysts included three catalysts that generate lower Mw polyethylene, (CpMe 5 )(1-MeInd)ZrCl 2 (A) 306 , )1-EtInd) 2 ZrCl 2 (B) 308 , and (Me 4 Cp)(1,3-Me 2 Ind)Zr Cl 2 (E) 310 .
  • the catalysts also included a catalyst that generates a middle Mw polyethylene, (PrCp) 2 HfF 2 (I) 312 .
  • Table 2 contains data on the dependence of Mw on H 2 /C 2 level.
  • the equations from Table 3 can be used to predict the amounts of (1-EtInd) 2 ZrCl 2 needed in a combination with the catalyst (PrCp) 2 HfF 2 to make an overall resin with Mw of 100 Kg/mol at four different H 2 levels. These values may be used to set initial control points, for example, if (PrCp) 2 HfF 2 is used as a supported catalyst component, and (1-EtInd) 2 ZrCl 2 is a solution catalyst component, to be added as a trim catalyst. In this embodiment, the amount of the (1-EtInd) 2 ZrCl 2 catalyst that is added may be controlled to achieve Mw and other performance targets. Results for various combinations are shown in Table 4.
  • HfP is capable of polymerizing ethylene and mixtures of ethylene and comonomers in the presence of an activator and a support, a cocatalyst, or both.
  • the activator and support may be the same or different. Multiple activators, supports and or cocatalysts may be used simultaneously. Cocatalysts may be added to modify any of the ingredients.
  • the descriptor catalyst, HfP, activator, supports and or cocatalysts refers to the actual compounds and also solutions of these compounds in hydrocarbon solvents.
  • the catalysts should be soluble in alkane solvents such as hexane, paraffinic solvents, and mineral oil.
  • alkane solvents such as hexane, paraffinic solvents, and mineral oil.
  • the solubility may be greater than 0.0001 wt. %, greater than 0.01 wt. %, greater than 1 wt. %, or greater than 2%.
  • Toluene may also be used as a solvent as the catalyst may be more soluble in an aromatic solvent
  • a combination of HfP, an activator (MAO), and a support (silica) was reacted with trim catalysts in hydrocarbon solvents to yield a polymerization catalyst with a different polymerization behavior than expected from the combination of the individual components. More specifically, the molecular weight distribution for a polymer generated by the co-supported co-catalysts is broader than can be achieved by mixtures of polymers formed from the individual component catalysts. This change in polymerization behavior is exemplified by changes in the MWD, the CD, or MWD and CD of polymers formed by the mixture of HfP and the selected cocatalysts. Thus, combining catalysts, HfP, activator and optionally a support, additional cocatalysts, or both, in hydrocarbon solvents in an in-line mixer immediately prior to a polymerization reactor yields a new polymerization catalyst.
  • any sequence of the combination of catalysts, HfP, activator and optionally a support, additional cocatalysts, or both, in hydrocarbon solvents may be used.
  • the catalysts may be added to a mixture that includes HfP, activator and optionally a support, additional cocatalysts, or both.
  • catalysts and cocatalysts may be added to a mixture of ⁇ HfP, activator and optionally a support ⁇ .
  • catalysts and HfP may be added to a mixture that includes ⁇ activator and optionally a support and cocatalysts ⁇ .
  • catalysts HfP, the activator and optionally a support, additional cocatalysts or both, in hydrocarbon solvents then obtain a dry catalyst from the mixture.
  • This dry mixture may be fed directly, or as a slurry, into a polymerization reactor.
  • the change in the MWD and CD upon using the catalysts and HfP can be controlled by changing the ratio of the catalysts to HfP.
  • the MWD and CD is that of HfP.
  • the MWD and CD is that generated by the catalysts themselves.
  • Changing the ratio of catalysts changes the MWD and CD from that of the parents. The ratio can be changed to target specific MWD and CD targets.
  • Catalysts can be chosen to control the change in MWD or CD of the polymer formed. Employing catalysts that yield lower or higher molecular weight polymers than HfP will broaden the molecular weight distribution.
  • the response of the Mw of polymers made from the single components versus H2/C2 can be used as a guide for the selection. For example, a catalyst having less response to hydrogen than HfP will yield a higher Mw than a polymer produced by HfP by itself, as shown in FIG. 2 . Further, a catalyst having a higher response to hydrogen than HfP will, in a combination with HfP, yield a lower Mw than HfP by itself.
  • catalysts may be selected to change the composition distribution. For example, employing catalysts that incorporate less or more comonomer than HfP will broaden the composition distribution.
  • a rough guide to this effect is the relative gas C6/C2 ratios required to prepare an approximately 0.92 D resin from different catalysts. Those catalysts that give larger differences in C6/C2 gas ratios from HfP will broaden the CD more.
  • Molecular weight distributions can also be changed by employing a catalyst that yields a different MWD but similar average molecular weight to that from HfP.
  • the combination of catalysts with HfP can yield a MWD that is larger than expected from the theoretical combination of the individual catalysts.
  • Desirable materials based on an HfP base catalyst are made when the Mw and comonomer incorporation abilities of the catalysts are both higher than HfP.
  • desirable materials are also formed when the Mw and comonomer incorporation abilities of the catalysts are both lower than HfP.
  • desirable materials are made when the Mw and of the catalysts are similar to and the comonomer incorporation abilities lower than HfP.
  • FIG. 4 is a flow chart of a method 400 for making a co-supported polymerization catalyst.
  • the method 400 begins at block 402 with the generation of a plot of hydrogen/ethylene ratio versus the reciprocal of molecular weight of a polymer generated by each one of a number of catalysts. As discussed herein, the slope of each plot indicates the response of the corresponding catalyst to a hydrogen level.
  • a value is determined for the comonomer/ethylene ratio for each of the catalysts that can be used to achieve a single target density, such as 0.92.
  • the value of the ratio used to achieve the target density indicates the ability of the catalyst to incorporate comonomer.
  • a first catalyst is selected for the co-supported polymerization catalyst.
  • the first catalyst can be a commonly used commercial catalyst, or may be selected to have a low or a high ability to incorporate comonomer and a high or low response to hydrogen.
  • a second catalyst is selected for the co-supported polymerization catalyst.
  • the second catalyst can be selected to have a slope of the plot for the hydrogen/ethylene ratio versus the reciprocal of molecular weight that is at least about 1.5 times as large as the slope of the plot for the first catalyst. Further, the second catalyst can be selected to have a value for the comonomer/ethylene ratio that is less than about 0.5 as large as comonomer/ethylene ratio of the first catalyst.
  • the first catalyst and the second catalyst can be co-supported on a single support to create the co-supported polymerization catalyst, for example, using the trim techniques described herein, among others.
  • the solid was isolated by filtration, washed with cold pentane (2 ⁇ 50 mL) and dried under vacuum to give 29.2 g solid with a rac/meso ration of 0.94:1.
  • the isolated solid was extracted with warm hexane (ca. 150 mL) filtered away from a small amount of pink solid. The volume was reduced to about 125 mL and the solution was treated with trimethylsilylchloride (2.0 mL). The solution was filtered, concentrated to about 100 mL, heated to re-dissolve the precipitated product and allowed to cool slowly. After sitting overnight, the flask was cooled to ⁇ 20 C which caused some pink solid to precipitate. The flask was warmed to 55° C.
  • iodomethane (2.0 ml, 32.1 mmol) was dissolved in 80 ml dry diethyl ether in a 250 ml round bottom flask with magnetic spinbar. Flask was placed in a isohexane cold bath ( ⁇ 25° C.) in a wide mouth dewar. In a separate 100 ml Erlenmeyer flask, a room temperature solution of 1-methylindenyl lithium (3.50 g, 25.7 mmol) was prepared in 50 ml dry diethyl ether, affording a yellow solution. Slow, dropwise addition of indenyl lithium solution to the cold, stirred solution of iodomethane was performed over 15 min.
  • Ineos ES757 silica (3969 g) was charged into a dehydrator (6 ft length, 6.25 in diameter) equipped with a 3-zone heater then fluidized with dry N2 gas at a flow rate of 0.12 ft 3 /s. Afterwards, the temperature was raised to 200° C. in a 2 h period. After holding at 200° C. for 2 h, the temperature was raised to 610° C. in a 6 h period. After holding at 610° C. for 4 h, the temperature was allowed to cool to ambient temperature over a 12 h period. The silica was transferred under N 2 to an APC can then stored under N 2 pressure (20 psig).
  • a 2 L autoclave Under a N 2 atmosphere, a 2 L autoclave was charged with dry salt (200 g) and SMAO (3 g). At a pressure of 2 psig N 2 , dry, degassed 1-hexene (see Table 6) was added to the reactor with a syringe. The reactor was sealed, heated to 80° C. while stirring the bed, then charged with N 2 to a pressure of 20 psig. Then, solid catalyst was injected into the reactor with ethylene at a pressure of 220 psig; ethylene flow was allowed over the course of the run. The temperature was raised to 85° C. Hexene was fed into the reactor as a ratio to ethylene flow (0.08 g/g).
  • Hydrogen was fed into the reactor as a ratio to ethylene flow per the description in the table.
  • the hydrogen and ethylene ratios were measured by on-line GC analysis. Polymerizations were halted after 1 h by venting the reactor, cooling to room temperature then exposing to air. The salt was removed by stirring the crude product in water. The polymer was obtained by filtration then drying in a vacuum oven.
  • the two 75/25 batches were combined in a 4 L Nalgene bottle and manually mixed by spinning and shaking the bottle.
  • the two 50/50 batches were also mixed in the same manner.
  • the feed stock slurry was prepared by first adding 10 wt % MAO (24.7 lbs), toluene (35.8 lbs) and Cabosil TS-610 (3.4 lbs) to a 10 gallon feed tank. The mixture was stirred overnight at room temperature. HfP (III) (28.75 g, 0.06798 mol) was added then the resulting slurry was mixed for another hour at ⁇ 38-40° C. before spraying. The catalyst was spray dried at a slurry feed rate of 93 lb/h, 90% atomizer speed, and outlet temperature of 80° C. in a procedure similar to reported in U.S. Pat. No. 7,276,566 B2. Yield was 2289 g (85%). Analytical data are reported in Table 9.
  • the polymerization was conducted in a continuous gas phase fluidized bed reactor having a straight section of 24 inch (61 cm) diameter with a length of approximately 11.75 feet (3.6 m) and an expanded section of 10.2 feet (3.1 m) length and 4.2 feet (1.3 m) diameter at the largest width.
  • the fluidized bed is made up of polymer granules.
  • the gaseous feed streams of ethylene and hydrogen together with liquid 1-hexene were mixed together in a mixing tee arrangement and introduced below the reactor bed into the recycle gas line.
  • the individual flow rates of ethylene, hydrogen and 1-hexene were controlled to maintain fixed composition targets.
  • the ethylene concentration was controlled to maintain a constant ethylene partial pressure.
  • They hydrogen was controlled to maintain a constant hydrogen to ethylene mole ratio.
  • the concentrations of all gasses were measured by an on-line gas chromatograph to ensure relatively constant composition in the recycle gas stream.
  • the solid catalyst was injected directly into the fluidized bed using purified nitrogen as a carrier. Its rate of injection was adjusted to maintain a constant production rate of the polymer.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity 1-3 ft/sec (0.3 to 0.9 m/sec).
  • the reactor was operated at a total pressure of 300 psig (2068 kPa gauge). To maintain a constant reactor temperature, the temperature of the recycle gas was continuously adjusted up or down to accommodate any changes in the rate of heat generation due to the polymerization.
  • a solution of anti-static agents in hexane (1:1 Aluminum stearate: N-nonyldiethanolamine at 20 wt %) was fed into the reactor using a mixture of iso-pentane and nitrogen at such a rate as too maintain ca. 30 ppm anti-static agents in the fluidized bed.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the product was removed semi-continuously via a series of valves into a fixed volume chamber, which was simultaneously vented back to the reactor to allow highly efficient removal of the product, while at the same time recycling a large portion of the unreacted gases back to the reactor.
  • This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen to deactivate any trace quantities of residual catalyst and cocatalyst.
  • a gas phase fluidized bed reactor of 0.35 meters internal diameter and 2.3 meters in bed height was utilized for polymerizations, with the results shown in Table 11.
  • the fluidized bed was made up of polymer granules and the gaseous feed streams of ethylene and hydrogen together with liquid 1-hexene comonomer were introduced below the reactor bed into the recycle gas line.
  • the individual flow rates of ethylene, hydrogen and 1-hexene were controlled to maintain fixed composition targets.
  • the ethylene concentration was controlled to maintain a constant ethylene partial pressure.
  • the hydrogen was controlled to maintain constant hydrogen to ethylene mole ratio.
  • the concentrations of all the gases were measured by an on-line gas chromatograph to ensure relatively constant composition in the recycle gas stream.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by the continuous flow of the make-up feed and recycle gas through the reaction zone. A superficial gas velocity of 0.6-0.9 meters/sec was used to achieve this.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the polymer production rate was in the range of 15-25 kg/hour.
  • the product was removed semi-continuously via a series of valves into a fixed volume chamber. This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen to deactivate any trace quantities of residual catalyst.
  • the solid catalyst was dispersed in degassed and dried mineral oil as a nominal 18 wt % slurry and contacted with the trim catalyst solution for a few seconds to minutes before being injected directly into the fluidized bed using purified nitrogen and isopentane as carriers in a manner that produces an effervescence of nitrogen in the liquid and spray to aid in dispersing the catalyst.
  • the trim catalyst was provided initially as a solution, and substantially diluted with isopentane to a concentration of about 0.015 wt % before being mixed in-line with the slurry catalyst component in a continuous manner prior to injection to the reactor.
  • the relative feeds of the slurry catalyst and the trim catalyst were controlled to achieve an aim target feed ratio of their active polymerization metals, and the feeds adjusted accordingly for overall polymer production rate and the relative amounts of polymer produced by each catalyst based somewhat on polymer flow index MFR and density, while also manipulating reaction temperature and the gas compositions in the reactor.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity in about the range of 2.0 to 2.2 ft/sec (0.61 to 0.67 m/sec).
  • the reactor was operated at a total pressure of about 350 psig (2413 kPa gauge).
  • the temperature of the recycle gas was continuously adjusted up or down by passing the recirculating gas through the tubes of a shell-and-tube heat exchanger with cooling water on the shell-side to accommodate any changes in the rate of heat generation due to the polymerization.
  • a slurry mixture of anti-static agents in degassed and dried mineral oil (1:1 Aluminum stearate: N-nonyldiethanolamine at 20 wt % concentration) was fed into the reactor using a mixture of iso-pentane and nitrogen at such a rate as to achieve a concentration of between 38 and 123 ppmw anti-static agents in the fluidized bed.
  • Isopentane and/or nitrogen was optionally employed to assist in conveying and dispersing the slurry mixture of anti-static into the reactor fluidized bed via a 1 ⁇ 8 inch to 3/16 inch OD injection tube thief extending a few inches into the bed from the reactor side wall.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the product was removed semi-continuously via a series of valves into a fixed volume discharge chamber. This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen immediately on discharge to a receiving fiberpak drum to deactivate any trace quantities of residual catalyst and cocatalyst.

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US17/067,287 Abandoned US20210024670A1 (en) 2014-02-11 2020-10-09 Method to prepare ethylene copolymers
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US16/278,212 Active 2035-05-22 US11034783B2 (en) 2014-02-11 2019-02-18 Method of producing polyethylene and polyethylene thereof
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