WO2017058391A1 - Procédé de polymérisation à l'aide de composés bisphénolate supportés sur des supports de silicate stratifié traité par un organoaluminium - Google Patents

Procédé de polymérisation à l'aide de composés bisphénolate supportés sur des supports de silicate stratifié traité par un organoaluminium Download PDF

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WO2017058391A1
WO2017058391A1 PCT/US2016/047888 US2016047888W WO2017058391A1 WO 2017058391 A1 WO2017058391 A1 WO 2017058391A1 US 2016047888 W US2016047888 W US 2016047888W WO 2017058391 A1 WO2017058391 A1 WO 2017058391A1
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layered silicate
substituted
group
heteroatom
catalyst
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PCT/US2016/047888
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English (en)
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Crisita Carmen H. ATIENZA
Matthew W. Holtcamp
Xuan YE
Gregory S. DAY
David A. Cano
Machteld M.W. MERTENS
Gerardo J. MAJANO SANCHEZ
Rohan A. HULE
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Exxonmobil Chemical Patents Inc.
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Publication of WO2017058391A1 publication Critical patent/WO2017058391A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2410/00—Features related to the catalyst preparation, the catalyst use or to the deactivation of the catalyst
    • C08F2410/07—Catalyst support treated by an anion, e.g. Cl-, F-, SO42-
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65912—Component covered by group C08F4/64 containing a transition metal-carbon bond in combination with an organoaluminium compound
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65916—Component covered by group C08F4/64 containing a transition metal-carbon bond supported on a carrier, e.g. silica, MgCl2, polymer

Definitions

  • TITLE Polymerization Process Using Bis Phenolate Compounds Supported on Organoaluminum Treated Layered Silicate Supports
  • This invention relates to supported bisphenolate compounds useful for the polymerization of olefins, in particular ethylene, where the catalyst support comprises a layered silicate and an inorganic oxide.
  • This invention also relates to polymerization processes using these supported bisphenolate compounds, in particular, gas phase polymerization processes.
  • Low density polyethylene is generally prepared at high pressure using free radical initiators, or in gas phase processes using Ziegler-Natta or vanadium catalysts, and typically has a density in the range of 0.916 to 0.950 g/cm 3 .
  • Typical low density polyethylene produced using free radical initiators is known in the industry as "LDPE”.
  • LDPE is also known as "branched” or “heterogeneously branched” polyethylene because of the relatively large number of long chain branches extending from the main polymer backbone.
  • LLDPE linear low density polyethylene
  • Polyethylenes having still greater density are the high density polyethylenes (“HDPEs”), i.e., polyethylenes having densities greater than 0.940 g/cm 3 , and are generally prepared with Ziegler-Natta catalysts.
  • Very low density polyethylenes (“VLDPEs”) are also known.
  • VLDPEs can be produced by a number of different processes yielding polyethylenes having a density less than 0.916 g/cm 3 , typically 0.890 to 0.915 g/cm 3 or 0.900 to 0.915 g/cm 3 .
  • LDPE which is soft, ductile, and flexible, is additionally utilized for strong, elastic goods, such as screw caps, lids, and coatings.
  • JP2011-089019A discloses a bridged metallocene in combination with a cocatalyst (a modified clay mineral, an alkyl alumoxane or an ionized ionic compound) and an organoaluminum compound for olefin polymerization which can produce a polyolefin which possesses long chain branching with high activity.
  • a cocatalyst a modified clay mineral, an alkyl alumoxane or an ionized ionic compound
  • organoaluminum compound for olefin polymerization which can produce a polyolefin which possesses long chain branching with high activity.
  • US 5,928,982 and US 5,973,084 report olefin polymerization catalysts containing an acid or salt-treated (or a combination of both) ion exchange layered silicate, containing less than 1% by weight water, an organoaluminum compound and a metallocene.
  • WO 01/42320 Al discloses combinations of clay or clay derivatives as a catalyst support, an activator comprising any Group 1-12 metal or Group 13 metalloid, other than organoaluminum compound, and a Group 3-13 metal complex.
  • US 6,531,552 and EP 1 160 261 Al report an olefin polymerization catalyst of an ion-exchange layered compound having particular acid strength and acid site densities.
  • US 2003/0027950 Al reports an olefin polymerization catalyst utilizing ion-exchange layered silicates with a specific pore size distribution and having a carrier strength within a specific range.
  • US 7,220,695 discloses catalyst systems comprising, inter alia, metallocene catalysts and supported activator systems comprising an ion-exchange layered silicate, an organoaluminum compound, and a heterocyclic organic compound, see Example 7 et seq.
  • US 6,559,090 discloses a coordinating catalyst system comprising at least one metallocene or constrained geometry pre-catalyst transition metal compound, (e.g., di-(n- butylcyclopentadienyl)zirconium dichloride), at least one support-activator (e.g., spray dried silica/clay agglomerate), and, optionally, at least one organometallic compound (e.g., triisobutyl aluminum), in controlled amounts, and methods for preparing the same.
  • transition metal compound e.g., di-(n- butylcyclopentadienyl)zirconium dichloride
  • support-activator e.g., spray dried silica/clay agglomerate
  • organometallic compound e.g., triisobutyl aluminum
  • This invention relates to a process to polymerize olefins comprising: i) contacting olefins with a catalyst system comprising: 1) support comprising an organoaluminum treated layered silicate and an inorganic oxide and 2) bisphenolate catalyst compound represented by the Formula (A):
  • M is a Group 4 transition metal
  • X 1 and X 2 are, independently, a univalent Ci to C2 0 hydrocarbyl radical, a Ci to C2 0 substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or X 1 and X 2 join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure;
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 and R 10 is, independently, a hydrogen, a Ci to C 40 hydrocarbyl radical, a Ci to C 4 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof;
  • Q is a neutral donor group
  • J is a C 7 to C 6 o fused polycyclic group, which optionally comprises up to 20 atoms from groups 15 and 16, where at least one ring is aromatic and where at least one ring, which may or may not be aromatic, has at least five members;
  • G is as defined for J or may be hydrogen, a Ci to C 6 o hydrocarbyl radical, a Ci to C 6 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or may independently form a C 4 to C 6 o cyclic or polycyclic ring structure with R 6 , R 7 , or R 8 or a combination thereof; and
  • Y is a divalent Ci to C2 0 hydrocarbyl or divalent Ci to C2 0 substituted hydrocarbyl.
  • This invention also relates to a process to polymerize olefins comprising: i) contacting olefins with a catalyst system comprising: 1) support comprising an organoaluminum treated layered silicate and an inorganic oxide and 2) bisphenolate catalyst compound represented by the Formula (A):
  • M is a Group 4 transition metal
  • X 1 and X 2 are, independently, a univalent Ci to C2 0 hydrocarbyl radical, a Ci to C2 0 substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or X 1 and X 2 join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure;
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 ,and R 10 is, independently, a hydrogen, a Ci to C 40 hydrocarbyl radical, a Ci to C 4 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof;
  • Q is a neutral donor group
  • J is a C 7 to C 6 o fused polycyclic group, which optionally comprises up to 20 atoms from groups 15 and 16, where at least one ring is aromatic and where at least one ring, which may or may not be aromatic, has at least five members;
  • G is as defined for J or may be hydrogen, a Ci to C 6 o hydrocarbyl radical, a Ci to C 6 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or may independently form a C 4 to C 6 o cyclic or polycyclic ring structure with R 6 , R 7 , or R 8 ' or a combination thereof; and
  • Y is a divalent Ci to C2 0 hydrocarbyl or divalent Ci to C2 0 substituted hydrocarbyl.
  • This invention also relates to a supported catalyst system comprising a bisphenolate catalyst compound described above and a support comprising an organoaluminum (preferably alkylaluminum) treated layered silicate and an inorganic oxide.
  • organoaluminum preferably alkylaluminum
  • This invention also relates to supported catalyst systems comprising bisphenolate compounds described above supported on particles of an agglomerate of an inorganic oxide and an organoaluminum (preferably alkylaluminum) treated layered silicate, where the support has been spray dried prior to contact with the organoaluminum.
  • organoaluminum preferably alkylaluminum
  • This invention relates to catalyst systems comprising: 1) a support comprising an organoaluminum treated layered silicate and an inorganic oxide and 2) bisphenolate compound represented by the formula described above.
  • Catalyst productivity is a measure of how many grams of polymer (P) are produced using a polymerization catalyst comprising W g of catalyst (cat), over a period of time of T hours; and may be expressed by the following formula: P/(T x W) and expressed in units of gP/gcat/hr.
  • an "olefin,” alternatively referred to as “alkene,” is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond.
  • alkene is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond.
  • the olefin present in the polymer is the polymerized form of the olefin.
  • ethylene content of 35 wt% to 55 wt%
  • the mer unit in the copolymer is derived from ethylene in the polymerization reaction and said derived units are present at 35 wt% to 55 wt%, based upon the weight of the copolymer.
  • a "polymer” has two or more of the same or different mer units.
  • a “homopolymer” is a polymer having mer units that are the same.
  • a “copolymer” is a polymer having two or more mer units that are different from each other.
  • a “terpolymer” is a polymer having three mer units that are different from each other.
  • "Different,” as used to refer to mer units indicates that the mer units differ from each other by at least one atom or are different isomerically. Accordingly, the definition of polymer, as used herein, includes co- and ter- polymers and the like and the definition of copolymer, as used herein, includes terpolymers and the like.
  • An ethylene polymer is a polymer comprising more than 50 mol% ethylene
  • a propylene polymer is a polymer comprising more than 50 mol% propylene, and so on.
  • Mn is number average molecular weight
  • Mw is weight average molecular weight
  • Mz is z average molecular weight
  • wt% is weight percent
  • mol% is mole percent
  • vol% is volume percent
  • mol mole.
  • PDI polydispersity index
  • a "catalyst system” is a combination of at least one catalyst compound, at least one activator, at least one support material, and optional co-activator.
  • An "anionic ligand” is a negatively charged ligand which donates one or more pairs of electrons to a metal ion.
  • a “neutral donor ligand” is a neutrally charged ligand which donates one or more pairs of electrons to a metal ion.
  • dme 1,2- dimethoxyethane
  • Me is methyl
  • Ph is phenyl
  • Et is ethyl
  • Pr is propyl
  • iPr is isopropyl
  • n-Pr normal propyl
  • Bu is butyl
  • iBu is isobutyl
  • tBu is tertiary butyl
  • p-tBu is para-tertiary butyl
  • nBu normal butyl
  • TMS is trimethylsilyl
  • TiBAl is triisobutylaluminum
  • TNOAL is tri(n- octyl) aluminum
  • MAO is methylalumoxane
  • p-Me is para-methyl
  • Bn is benzyl (i.e., CH 2 Ph)
  • THF also referred to as thf
  • thf is tetrahydrofuran
  • tol is toluene
  • EtOAc is eth
  • Room temperature (RT) is 23°C unless otherwise indicated.
  • substituted means that a hydrogen has been replaced with a heteroatom, a heteroatom-containing group, or a hydrocarbyl group.
  • bromo-cyclopentadiene is cyclopentadiene substituted with a bromine group.
  • hydrocarbyl radical is defined to be a radical of carbon and hydrogen, preferably a C ⁇ to Cioo radical of carbon and hydrogen, that may be linear, branched, or cyclic, and when cyclic, aromatic or non- aromatic.
  • Substituted hydrocarbyl radicals are hydrocarbyl radicals in which at least one hydrogen atom of the hydrocarbyl radical has been substituted with a heteroatom or heteroatom-containing group, such as a group having at least one functional group such as NR*2, OR*, SeR*, TeR*, PR* 2 , AsR* 2 , SbR* 2 , SR*, BR* 2 , SiR*3, GeR* 3 , SnR* 3 , PbR* 3 , and the like, or where at least one heteroatom has been inserted within a hydrocarbyl ring.
  • a heteroatom or heteroatom-containing group such as a group having at least one functional group such as NR*2, OR*, SeR*, TeR*, PR* 2 , AsR* 2 , SbR* 2 , SR*, BR* 2 , SiR*3, GeR* 3 , SnR* 3 , PbR* 3 , and the like, or where at least
  • complex is also often referred to as catalyst precursor, pre-catalyst, catalyst, catalyst compound, transition metal compound, or transition metal complex. These words are used interchangeably. Activator and cocatalyst are also used interchangeably.
  • a scavenger is a compound that is typically added to facilitate polymerization by scavenging impurities. Some scavengers may also act as chain transfer agents. Some scavengers may also act as activators and may be referred to as co-activators. A co-activator, that is not a scavenger, may also be used in conjunction with an activator in order to form an active catalyst. In some embodiments, a co-activator can be pre-mixed with the transition metal compound to form an alkylated transition metal compound.
  • scavengers include, but are not limited to, trialkylaluminums, methylalumoxanes, modified methylalumoxanes, MMAO-3A (Akzo Nobel), bis(diisobutylaluminum)oxide (Akzo Nobel), tri(n-octyl)aluminum, triisobutylaluminum, and diisobutylaluminum hydride.
  • aryl or "aryl group” means a six-carbon aromatic ring and the substituted variants thereof, including but not limited to, phenyl, 2-methyl-phenyl, xylyl, 4- bromo-xylyl.
  • heteroaryl means an aryl group where a ring carbon atom (or two or three ring carbon atoms) has been replaced with a heteroatom, preferably N, O, or S.
  • ring atom means an atom that is part of a cyclic ring structure.
  • a benzyl group has six ring atoms and tetrahydrofuran has 5 ring atoms.
  • a "ring carbon atom” is a carbon atom that is part of a cyclic ring structure.
  • a benzyl group has six ring carbon atoms and para-methylstyrene also has six ring carbon atoms.
  • a heterocyclic ring is a ring having a heteroatom in the ring structure as opposed to a heteroatom substituted ring where a hydrogen on a ring atom is replaced with a heteroatom.
  • tetrahydrofuran is a heterocyclic ring and 4-N,N-dimethylamino- phenyl is a heteroatom substituted ring.
  • Aromatic means a cyclic hydrocarbyl with conjugated double bonds, such as benzene or cyclopentadiene.
  • aromatic also refers to pseudoaromatic cyclic groups which are cyclic substituents that have similar properties and structures (nearly planar) to aromatic ligands, but are not by definition aromatic.
  • continuous means a system that operates without interruption or cessation.
  • a continuous process to produce a polymer would be one where the reactants are continually introduced into one or more reactors and polymer product is continually withdrawn.
  • agglomerate refers to a material comprising an assembly, of primary particles held together by adhesion, i.e., characterized by weak physical interactions such that the particles can easily be separated by mechanical or chemical forces.
  • a carbazole radical a hydrocarbyl radical
  • each R 1 through R 8 is, independently, a hydrogen, a Ci to C 4 o hydrocarbyl radical, a substituted Ci to C 4 o hydrocarbyl radical (such as a functional group comprising elements from group 13 to 17 of the periodic table of the elements), or two or more of R 1 to R 8 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof.
  • a substituted carbazole is one where at least one of R 1 to R 8 is not H.
  • each R through R is, independently, a hydrogen, a Ci to C 4 o hydrocarbyl radical, a substituted Ci to C 4 o hydrocarbyl radical (such as a functional group comprising elements from group 13 to 17 of the periodic table of the elements), or two or more of R 1 to R 8 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof;
  • R* is a hydrogen, a Ci to C 4 o hydrocarbyl radical, a substituted Ci to C 4 o hydrocarbyl radical (preferably R* is methyl, phenyl, tolyl, substituted phenyl, or substituted tolyl).
  • a substituted flourenyl is one where at least one of R*, or R 1 to R 8 is not H.
  • a bulky functional group is defined as a functional group having a molecular size greater than or equal to an isopropyl moiety. Accordingly, for purposes herein a bulky functional group includes substituted or unsubstituted bulky aliphatic radicals having three carbons or more, bulky alicyclic radicals having three carbons or more, and/or bulky aromatic radicals having 5 carbons or more, each having a molecular size greater than or equal to an isopropyl moiety.
  • Molecular volume is used herein as an approximation of spatial steric bulk of an activator molecule in solution. Comparison of substituents with differing molecular volumes allows the substituent with the smaller molecular volume to be considered “less bulky” in comparison to the substituent with the larger molecular volume. Conversely, a substituent with a larger molecular volume may be considered “more bulky” than a substituent with a smaller molecular volume.
  • Molecular volume may be calculated as reported in "A Simple "Back of the Envelope” Method for Estimating the Densities and Molecular Volumes of Liquids and Solids," Journal of Chemical Education, Vol. 71, No. 11, November 1994, pp. 962-964.
  • V s is the sum of the relative volumes of the constituent atoms, and is calculated from the molecular formula of the substituent using the following table of relative volumes. For fused rings, the V s is decreased by 7.5% per fused ring.
  • This invention relates to catalyst systems comprising: 1) a support comprising an organoaluminum treated layered silicate and an inorganic oxide and 2) bisphenolate compound represented by the Formula (A) below.
  • This invention also relates to a process to polymerize olefins comprising: i) contacting olefins with catalyst systems comprising: 1) a support comprising an organoaluminum treated layered silicate and an inorganic oxide and 2) bisphenolate compound represented by the Formula (A):
  • M is a group 4 transition metal
  • X 1 and X 2 are, independently, a univalent Ci to C2 0 hydrocarbyl radical, a Ci to C2 0 substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or X 1 and X 2 join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure;
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 , and R 10 is, independently, a hydrogen, a Ci to C 40 hydrocarbyl radical, a Ci to C 4 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof;
  • Q is a neutral donor group
  • J is a C 7 to C 6 o fused polycyclic group, which optionally comprises up to 20 atoms from groups 15 and 16, where at least one ring is aromatic and where at least one ring, which may or may not be aromatic, has at least five members;
  • G is as defined for J or may be hydrogen, a Ci to C 6 o hydrocarbyl radical, a Ci to C 6 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or may independently form a C 4 to C 6 o cyclic or polycyclic ring structure with R 6 , R 7 , or R 6 or a combination thereof; and
  • Y is a divalent Ci to C2 0 hydrocarbyl or divalent Ci to C2 0 substituted hydrocarbyl.
  • the catalyst system is substantially free of alumoxane. In a preferred embodiment of the invention, the catalyst system is substantially free of non-coordinating anion activators. In a preferred embodiment of the invention, the catalyst system is substantially free of alumoxane and non-coordinating anion activators.
  • This invention also relates to a process to prepare high molecular weight (Mw of 1,000,000 g/mol or more) ethylene polymers, preferably having excellent bulk density (0.25 g/cc or more), preferably without using additional activator such as an alumoxane and or a non-coordinating anion, comprising contacting ethylene and optional comonomer with a catalyst system comprising bisphenolate compound represented by the Formula A, as described herein, deposited on a support comprising organoaluminum treated layered silicate and an inorganic oxide.
  • Mw molecular weight
  • ethylene polymers preferably having excellent bulk density (0.25 g/cc or more
  • additional activator such as an alumoxane and or a non-coordinating anion
  • This invention also relates to any of the above processes where the support and or the supported catalyst system is present in the form of spherioid particles, preferably having an average particle size (D50) of 20 to 180 microns, alternately 55 to 180 microns, and a surface area of about 100 to about 200 m 2 /g and a pore volume of about 0.1 to about 0.4 cc/g.
  • D50 average particle size
  • This invention also relates to any of the above processes where the support and/or the supported catalyst system have an average aspect ratio (L/W) of 1 to 1.7 (alternately 1 to 1.6, alternately 1 to 1.5, alternately 1 to 1.4, alternately 1 to 1.3, and alternately 1 to 1.2).
  • L/W average aspect ratio
  • Average aspect ratio of the support and or supported catalyst systems is determined by averaging the aspect ratio (length versus width) of multiple particles as shown in Scanning Electron Micrographs. Several SEM photographs of the sample are taken and 35 particles of layered silicate are identified and measured. For each of the 35 particles, the longest dimension is identified by drawing a line between the two points at the edge of the particle which are the furthest apart ("length"). Then the shortest dimension is identified by drawing a line between the two points at the edge of the particle which are the least distance apart ("width"). Length is then divided by width to obtain aspect ratio. The average aspect ratio is calculated as the arithmetical mean based on the aspect ratio of the 35 particles. Image-Pro PlusTM v 7.0.0 is used for image analysis.
  • This invention also relates to any of the above processes where the support and/or the supported catalyst system is present in the form of spherioid particles, has an average aspect ratio (LAV) of 1 to 1.7 (alternately 1 to 1.6, alternately 1 to 1.5, alternately 1 to 1.4, alternately 1 to 1.3, alternately 1 to 1.2); has an average particle size (D50) of 20 to 180 microns, alternately 55 to 180 microns, has a surface area of about 100 to about 200 m 2 /g and has a pore volume of about 0.1 to about 0.4 cc/g.
  • LAV average aspect ratio
  • D50 average particle size
  • the catalyst system has an average aspect ratio (LAV) of 1 to 1.7, has an average particle size (D50) of 20 to 180 microns, and has a pore volume of about 0.1 to about 0.4 cc/g.
  • LAV average aspect ratio
  • D50 average particle size
  • Catalyst compounds suitable in the catalyst system herein typically comprise a transition metal com lex represented by the Formula (A):
  • M is a group 4 transition metal (preferably Hf, Zr, or Ti, preferably Hf or Zr);
  • X 1 and X 2 are, independently, a univalent Ci to C2 0 hydrocarbyl radical, a Ci to C2 0 substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or X 1 and X 2 join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure (preferably benzyl, methyl, ethyl, chloro, bromo and the like);
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 , and R 10 is, independently, a hydrogen, a Ci to C 40 hydrocarbyl radical, a substituted Ci to C 4 o hydrocarbyl radical, a heteroatom, a heteroatom- containing group (alternately each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 , and R 10 may be a functional group comprising of elements from groups 13 to 17), or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof (preferably H, methyl, ethyl, propyl and the like);
  • Q is a neutral donor group, preferably a neutral donor group comprising at least one atom from group 15 or 16;
  • J is a C7 to C 6 o fused polycyclic (e.g., having at least 2 ring structures) group, which, optionally, comprises up to 20 atoms from groups 15 and 16, where at least one ring is aromatic and where at least one ring, which may or may not be aromatic, has at least 5 members (preferably J comprises a five-membered ring (which may be saturated or aromatic) that is fused to at least one other cyclic group and is preferably bound to the rest of the ligand through the five-membered ring).
  • G is, independently, as defined for J, a hydrogen, a Ci to C 6 o hydrocarbyl radical, a substituted hydrocarbyl radical, a heteroatom, or a heteroatom-containing group, or may independently form a C 4 to C 6 o cyclic or polycyclic ring structure with R 6 , R 7 , or R 8 , or a combination thereof; and
  • Y is a divalent Ci to C2 0 hydrocarbyl or a substituted divalent hydrocarbyl group.
  • the catalyst system comprises a catalyst compound represented by the formula ( ⁇ ) or ( ⁇ ):
  • Q* is a group 15 or 16 atom (preferably N, O, S or P);
  • z is 0 or 1 ;
  • J* is CR" or N
  • G* is CR" or N
  • each R", R*, R 11 , R 12 , R 13 , R 14 , R 15 , R 16 , R 17 , R 18 , R 19 , R 20 , R 21 , R 22 , R 23 , R 24 , R 25 , R 26 , and R 27 is, independently, as defined for R 1 above.
  • M may be Hf , Ti or Zr.
  • each of X 1 and X 2 is independently selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms (such as methyl, ethyl, ethenyl and isomers of propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl, octadecyl, nonadecyl, eicosyl), hydrides, amides, alkoxides having from 1 to 20 carbon atoms, sulfides, phosphides, halides, sulfoxides, sulfonates, phosphonates, nitrates, carboxylate
  • Y is a divalent Ci to C 4 o hydrocarbyl radical or divalent substituted hydrocarbyl radical comprising a portion that comprises a linker backbone comprising from 1 to 18 carbon atoms linking or bridging between Q and N.
  • Y is a divalent Ci to C 4 o hydrocarbyl or substituted hydrocarbyl radical comprising a portion that comprises a linker backbone comprising from 1 to 18 carbon atoms linking Q and N wherein the hydrocarbyl comprises O, S, S(O), S(0) 2 , Si(R) 2 , P(R), N or N(R), wherein each R is independently a Ci to Ci 8 hydrocarbyl.
  • Y is selected from the group consisting of ethylene (- CH2CH2-) and 1 ,2-cyclohexylene. In an embodiment, Y is -CH2CH2CH2- derived from propylene. In an embodiment, Y is selected form the group consisting of Ci to C2 0 alkyl groups, such as divalent methyl, ethyl, ethenyl and isomers of propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl, octadecyl, nonadecyl, and eicosyl.
  • Ci to C2 0 alkyl groups such as divalent methyl, ethyl, ethenyl and isomers of
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 , and R 10 is, independently, a hydrogen, a Ci to C2 0 hydrocarbyl radical, a substituted Ci to C2 0 hydrocarbyl radical, or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof.
  • each R*, p p i p2 p 3 p 4 p 5 p 6 p 7 p 8 p 9 p 10 p l l p 12 p 13 p 14 p 15 p 16 p 17 p 18 p 19 p 20 p 21 R 22 , R 23 R 24 , R 25 , R 26 , and R 27 is, independently, hydrogen, a halogen, a Ci to C 30 hydrocarbyl radical, a Ci to C2 0 hydrocarbyl radical, or a Ci to C1 0 hydrocarbyl radical (such as methyl, ethyl, ethenyl and isomers of propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, penta
  • R 22 , R 23 R 24 , R 25 , R 26 , and R 27 is, independently, a substituted Ci to C 30 hydrocarbyl radical, a substituted Ci to C2 0 hydrocarbyl radical, or a substituted Ci to C1 0 hydrocarbyl radical (such as 4-fluorophenyl, 4-chlorophenyl, 4-bromophenyl, 4-methoxyphenyl, 4- trifluoromethylphenyl, 4-dimethylaminophenyl, 4-trimethylsilylphenyl, 4-triethylsilylphenyl, trifluoromethyl, fluoromethyl, trichloromethyl, chloromethyl, mesityl, methylthio, phenylthio, (trimethylsilyl)methyl, and (triphenylsilyl)methyl).
  • a substituted Ci to C 30 hydrocarbyl radical such as 4-fluorophenyl, 4-chlorophenyl, 4-bromophenyl, 4-meth
  • one or more of R*, R", R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 , R 10 , R 11 , R 12 , R 13 , R 14 , R 15 , R 16 , R 17 , R 18 , R 19 , R 20 , R 21 , R 22 , R 23 R 24 , R 25 , R 26 , and R 27 is a methyl radical, a fluoride, chloride, bromide, iodide, methoxy, ethoxy, isopropoxy, trifluoromethyl, dimethylamino, diphenylamino, adamantyl, phenyl, pentafluorphenyl, naphthyl, anthracenyl, dimethylphosphanyl, diisopropylphosphanyl, diphenylphosphanyl, methylthio, and phenyl
  • Q* is N, O, S, or P, preferably N, O, or S, preferably N or O, preferably N.
  • Q* is a group 15 atom, z is 1
  • Q* is a group 16 atom, z is 0.
  • Q is preferably a neutral donor group comprising at least one atom from group 15 or 16, preferably Q is NR' 2 , OR', SR', PR 2 , where R is as defined for R 1 (preferably R' is methyl, ethyl, propyl, isopropyl, phenyl, cyclohexyl or linked together to form a five-membered ring such as pyrrolidinyl or a six-membered ring such as piperidinyl), preferably the -(-Q-Y-)- fragment can form a substituted or unsubstituted heterocycle which may or may not be aromatic and may have multiple fused rings (for example see compound 7-Zr, 7-Hf in the examples below).
  • Q is preferably an amine, ether, or pyridine.
  • G* and J* are the same, preferably G* and J* are N, alternately G* and J* are CR'", where each R'" is H or a Ci to Ci 2 hydrocarbyl or substituted hydrocarbyl (such as methyl, ethyl, ethenyl and isomers of propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, trifluoromethylphenyl, tolyl, phenyl, methoxyphenyl, tertbutylphenyl, fluorophenyl, diphenyl, dimethylaminophenyl, chlorophenyl, bromophenyl, iodophenyl, (trimethylsilyl)phenyl, (triethylsilyl)phenyl, (triethylsilyl)phenyl, (tri
  • G and J are the same, preferably G and J are carbazolyl, substituted carbazolyl, indolyl, substituted indolyl, indolinyl, substituted indolinyl, imidazolyl, substituted imidazolyl, indenyl, substituted indenyl, indanyl, substituted indanyl, fluorenyl, or substituted fluorenyl.
  • G and J are different.
  • M is Zr or Hf; X 1 and X 2 are benzyl radicals; R 1 is a methyl radical; R 2 through R 27 are hydrogen; Y is ethylene (-CH 2 CH 2 -), Q*, G* and J* are N, and Rz* is methyl radical.
  • M is Zr or Hf
  • X 1 and X 2 are benzyl radicals
  • R 4 and R 7 are methyl radicals
  • R 1 through R 3 , R 5 through R 6 and R 8 through R 10 are hydrogen
  • Y is ethylene, (-CH 2 CH 2 -)
  • Q is an N-containing group
  • G and J are carbazolyl or fluorenyl.
  • G and J are carbazolyl and Q is an amine group; or, G and J are substituted fluorenyl and Q is an amine, ether or pyridine.
  • the catalyst complex is re resented by formula (IV) or (V):
  • Y is a Ci to C 3 divalent hydrocarbyl
  • Q 1 is NR 2 , OR', SR, PR' 2 , where R' is as defined for R 1 (preferably R' is methyl, ethyl, propyl, isopropyl, phenyl, cyclohexyl or linked together to form a five-membered ring such as pyrrolidinyl or a six-membered ring such as piperidinyl), alternately the -(-Q-Y-)- fragment can form a substituted or unsubstituted heterocycle which may or may not be aromatic and may have multiple fused rings
  • M is Zr, Hf or Ti and each X is, independently, as defined for X 1 above, preferably each X is benzyl, methyl, ethyl, chloride, bromide or alkoxide.
  • the transition metal compounds may be prepared by two general synthetic routes.
  • the amine bis(phenolate) ligands may be prepared by a one-step Mannich reaction from the parent phenol (Reaction A) or by a nucleophilic substitution reaction of the methylbromide derivative of the phenol (Reaction B).
  • the ligand is then typically reacted with the metal tetra-alkyl compound, e.g., tetrabenzyl, to yield the metal dibenzyl complex of the ligand (Reaction C);
  • M, Y, and Q are as defined for M, Y, and Q above, [H 2 CO] x is paraformaldehyde, Bn is benzyl, and each R is, independently, as defined for G or J above, provided that at least one R is as defined for J.
  • catalyst system includes transition metal complex/activator pair(s).
  • Catalyst system When “catalyst system” is used to describe such pair(s) before activation, it means the unactivated catalyst complex (pre-catalyst) together with an activator (e.g., the organoalumimun treated layered silicate) and, optionally, a co-activator.
  • an activator e.g., the organoalumimun treated layered silicate
  • co-activator e.g., the organoalumimun treated layered silicate
  • the transition metal compound may be neutral, as in a pre-catalyst, or a charged species with a counter ion as in an activated catalyst system.
  • the complexes described herein may be used in combination with one or more support-activators (e.g., the organoalumimun treated layered silicates described herein, which act as both supports and activators) for olefin polymerization, such as for ethylene-based polymers or propylene-based polymers, including ethylene-octene polymerization.
  • support-activators e.g., the organoalumimun treated layered silicates described herein, which act as both supports and activators
  • olefin polymerization such as for ethylene-based polymers or propylene-based polymers, including ethylene-octene polymerization.
  • this invention also relates to supported catalyst systems comprising: (i) at least one bisphenolate compound represented by Formula (A) (preferably ( ⁇ ), ( ⁇ ), (IV), or (V)) as described above; (ii) a support comprising an agglomerate of organoaluminum (preferably alkylaluminum) treated layered silicate material and inorganic oxide; and (iii) optionally, a cocatalyst.
  • the bisphenolate catalyst compound may be any of the compounds described above.
  • the organoaluminum (preferably alkylaluminum) treated layered silicate and optional cocatalyst/scavenger are discussed below.
  • catalyst is present on the support at from 0.01 wt% to 1 wt%, preferably 0.1 to 0.5 wt% of Ti, Zr, or Hf, based upon the weight of the catalyst, any activator, and support.
  • This invention relates to catalyst systems comprising organoaluminum (such as alkyl aluminum) treated layered silicates.
  • the layered silicate may be an ion exchange layered silicate.
  • Preferred ion-exchange layered silicates useful in the present invention are silicate compounds having a crystal structure wherein layers formed by strong ionic and covalent bonds are laminated in parallel with weak ionic bonding, and the ions contained between the layers are exchangeable. Most ion-exchange layered silicates naturally occur as the main component of clay minerals, but these ion-exchange layered silicates may be artificially synthesized materials.
  • Preferred ion-exchange layered silicates useful in this invention include natural or synthetic montmorillonite, nontronite, beidellite, volkonskoite, laponite, hectorite, saponite, sauconite, stevensite, vermiculite, halloysite, aluminate oxides, bentonite, kaolinite, dickite, smectic clays, mica, magadiite, kenyaite, octosilicate, kanemite, makatite, attapulgite, sepiolite, zeolitic layered materials (such as ITQ-2, MCM-22, and ferrierite precursors) and mixtures thereof.
  • montmorillonite nontronite, beidellite, volkonskoite, laponite, hectorite, saponite, sauconite, stevensite, vermiculite, halloysite, aluminate oxides
  • bentonite
  • the ion-exchange layered silicate is acidified (by contacting with an acid, such as sulfuric acid, hydrochloric acid, a carboxylic acid, an amino acid, or the like) or otherwise chemically treated (see US 6,559,090, especially columns 25 to 27).
  • an acid such as sulfuric acid, hydrochloric acid, a carboxylic acid, an amino acid, or the like
  • Preferred ion-exchange layered silicates useful in this invention include those having a 1 : 1 type structure or a 2: 1 type structure.
  • Examples of the ion-exchange layered silicate include layered silicates having a 1 : 1 type structure or a 2: 1 type structure as described in "Clay Mineralogy” written by R. E. Grim (published by McGraw Hill in 1968) and "Chemistry of Clays and Clay Minerals" written by A. C. Newman (published by John Wiley and Sons: New York in 1987).
  • the 1 : 1 type structure is a structure formed by laminating 1 : 1 layered structures having one layer of tetrahedral sheet and one layer of octahedral sheet combined as described in the above literature "Clay Mineralogy”
  • the 2: 1 type structure is a structure formed by laminating 2: 1 layered structures having one layer of octahedral sheet sandwiched between two layers of tetrahedral sheets.
  • ion- exchange layered silicate comprising the 1 : 1 layer as the main constituting layer
  • kaolin group silicates such as dickite, nacrite, kaolinite, metahalloysite, halloysite or the like
  • serpentine group silicates such as chrysotile, lizardite, antigorite, or the like.
  • ion-exchange layered silicate comprising the 2: 1 layer as the main constituting layer
  • smectite group silicates such as montmorillonite, beidellite, nontronite, saponite, hectorite, stephensite, or the like
  • vermiculite group silicates such as vermiculite or the like
  • mica group silicates such as mica, illite, sericite, glauconite, or the like
  • attapulgite sepiolite, palygorskite, bentonite, pyrophyllite, talc, chlorites, and the like.
  • Mixed layer silicates are also included.
  • an ion-exchange layered silicate having the 2: 1 type structure is preferable.
  • a smectite group silicate is used and in a particularly preferable example, the ion exchange layered silicate comprises montmorillonite.
  • Kinds of exchangeable cations are not specially limited, but the cations are preferably a metal of Group 1 of the Periodic Table of the Elements such as sodium or potassium, a metal of Group 2 of the Periodic Table of the Elements such as calcium or magnesium, or a transition metal such as iron, cobalt, copper, nickel, zinc, ruthenium, rhodium, palladium, silver, iridium, platinum, or gold, which are relatively easily available as industrial starting materials.
  • the ion-exchange layered silicate has an average particle size of from 0.02 to 200 microns, preferably from 0.25 to 100 microns, even more preferably 0.5 to 50 microns. In some embodiments, the ion exchange layered silicates have a bi-modal distribution, or even multi-modal distribution, of particle sizes.
  • the ion exchange layered silicate may be used in a dry state and/or may be used also in a slurry state in liquid and is preferably used as a free flowing powder after spray drying.
  • the shape of the ion-exchange layered silicate is not specially limited, and the shape may be a naturally occurring shape, an artificially synthesized shape or a shape of an ion-exchange layered silicate obtained after subjected to pulverizing, granulating, and classifying.
  • the ion exchange layered silicates are combined with other support type compounds, such as inorganic oxides, and used in this invention.
  • the ion-exchange layered silicate may be utilized as part of an agglomerate (as described in US 2003/0096698 and US 6,559,090, which are herein fully incorporated by reference), with at least one inorganic oxide component, such as S1O 2 , AI 2 O 3 , MgO, AIPO 4 , T1O 2 , ZrC> 2 , or & 2 (3 ⁇ 4.
  • an ion exchange layered silicate such as montmorillonite, may be combined with inorganic oxide, such as sodium silicate, and then combined with the organoaluminum compound (preferably, an alkylaluminum compound).
  • the organoalumimum treated layered silica support is a composite in the form of agglomerates of at least two components, namely, (A) at least one inorganic oxide component, such as silica or a silicon oxide, such as sodium silicate, and (B) at least one layered silicate component, typically an ion exchange layered silicate such as those described herein, particularly montmorillonite, particularly an ion exchange montmorillonite such as K10 or KSF.
  • the agglomerates are an intimate admixture of Components- A and -B.
  • the inorganic oxide Component-A of the agglomerate particles is derived from porous inorganic oxides including S1O 2 , AI 2 O 3 , AIPO 4 , MgO, T1O 2 , ⁇ (3 ⁇ 4; Na 2 SiC>3; and or mixed inorganic oxides including S1O 2 .AI 2 O 3 , MgO.Si0 2.
  • Particularly useful inorganic oxides include Group 1 and 2 silicates, such as sodium silicate, potassium silicate, calcium silicate, magnesium silicate, and mixtures thereof.
  • Component-B of the agglomerate particles is derived from layered silicate materials, particularly ion-exchange layered silicates, such as those described herein.
  • the layered silicate derived materials in Component-B can be amorphous or crystalline, preferably amorphous, and can be clay or clay minerals.
  • the layered silicate is a smectic clay.
  • Particularly useful ion-exchange layered silicates include magnesia, titania, montmorillonite (EP 0 51 1 665 Bl and US 5,965,477), phyllosilicate, zeolites, talc, clays (US 6,034, 187), and the like.
  • the ion-exchange layered silicates can be acid treated.
  • the ion-exchange layered silicates have an acidic pH, such as less than 7, alternately from 1 to 6, alternately from 3 to 5.
  • the agglomerates comprising Component- A and Component-B preferably contain 10 to 99.5 wt%, preferably 25 to 95 wt%, preferably 90 to 99 wt%, preferably 95 to 97 wt% of Component-B and 90 to 0.5 wt%, preferably 5 to 75 wt%, preferably 1 to 10 wt%, preferably 3 to 5 wt% of Component-A based upon the weight of Component-A and Component-B.
  • the agglomerates comprising Component-A and Component-B preferably contain 80 to 99.5 wt%, preferably 90 to 99 wt% of Component-B and preferably 20 to 0.5 wt%, preferably 10 to 1 wt% of Component-A based upon the weight of Component-A and Component-B.
  • the weight ratio of Component-A to Component-B in the agglomerate can vary typically from about 0.25: 100 to about 20: 100, preferably from about 0.5: 100 to about 10: 100, most preferably from about 1 : 100 to about 5: 100.
  • the agglomerates of the present invention preferably will exhibit a higher macropore content than the constituent particles as a result of the interparticle voids between the constituent particles. However, such interparticle voids may be partially or completely filled with the smaller secondary particles in other embodiments of the spray dried agglomerates.
  • the agglomeration of Components-A and -B may be carried out in accordance with the methods well known to the art, in particular, by such methods as spray drying.
  • the agglomerates typically have an average particle size of 1 to 1000 microns, preferably 50 to 500 microns, preferably 20 tol 80 microns, preferably 75 to 200 microns. In some embodiments the agglomerates have a bi-modal distribution, or even multi-modal distribution, of particle sizes.
  • Particle size also referred to as "average particle size,” “particle diameter,” or “average particle diameter,” is determined using a MastersizerTM 3000 (range of 1 to 3500 ⁇ ) available from Malvern Instruments, Ltd., Worcestershire, England. Unless otherwise stated, particle size is determined at D50. D50 is the value of the particle diameter at 50% in the cumulative distribution.
  • the agglomerates typically have a surface area of 100 to 300 m 2 /g, preferably 120 to 250 m 2 /g, preferably 130 to 220 m 2 /g, alternately 100 to 200 m 2 /g (as measured by BET).
  • the agglomerates typically have a pore volume of 0.1 to 0.5 cc/g, preferably 0.1 to 0.4 cc/g, preferably 0.15 to 0.35 cc/g (as measured by BET). Pore volume may be determined by the BJH method, but in event of conflict between the results of the two methods, the BET method shall be used. The BET method shall be used for the claims to this invention.
  • the agglomerates typically have a spheroidal shape.
  • the surface area (SA, also called the specific surface area or BET surface area), pore volume (PV) of support materials are to be determined by the Brunauer-Emmett- Teller (BET) method using adsorption-desorption of nitrogen (temperature of liquid nitrogen: 77 K) with a MICROMERITICS TRISTAR II 3020 instrument after degassing of the powders for 4 hrs at 350°C. More information regarding the method can be found, for example, in "Characterization of Porous Solids and Powders: Surface Area, Pore Size and Density," S. Lowell et al., Springer, 2004, PV refers to the total PV, including both internal and external PV.
  • BET Brunauer-Emmett- Teller
  • porosity of particles refers to the volume fraction or percentage of pore volume within a particle or body comprising a skeleton or matrix of the particle material, on the basis of the overall volume of the particle or body with respect to total volume.
  • the porosity and median pore diameter of particles are determined using mercury intrusion porosimetry.
  • Mercury intrusion porosimetry involves placing the sample in a penetrometer and surrounding the sample with mercury.
  • Mercury is a non-wetting liquid to most materials and resists entering voids, doing so only when pressure is applied.
  • the pressure at which mercury enters a pore is inversely proportional to the size of the opening to the void.
  • the agglomerates are typically a free flowing powder, preferably the agglomerate is formed into free flowing particles that have a pourability of 60 seconds or less as determined using ASTM 1895D.
  • free flowing is meant that the particles will flow through a funnel and yield a pourability value according to ASTM 1895D; preferably, the pourability value is about 50 seconds or less, more preferably about 30 seconds or less, still more preferably about 10 seconds or less, more preferably about 5 seconds or less, still more preferably about 1 second or less, when determined according to ASTM 1895D.
  • the agglomerates typically comprise from 0.1 mmol to 1 mmol aluminum that is derived from the aluminum alkyl per gram of support. Determining the aluminum content derived from the aluminum alkyl is done by titration using 1H NMR.
  • Processing of a shape of an ion-exchange layered silicate by granulating, pulverizing, or classifying may be carried out before chemical treatment (that is, the ion- exchange layered silicate having a shape previously processed may be subjected to the chemical treatment), or an ion-exchange layered silicate may be subjected to processing of a shape after chemical treatment.
  • Processing may occur before or after chemical treatment with an organoaluminum compound, an inorganic oxide and/or combination with a polymerization catalyst, however a particularly preferred method comprises dispersing the inorganic oxide and the ion-exchange layered silicate in water, thereafter spray drying, then contacting the spray dried particles with an organoaluminum compound, and thereafter contacting with polymerization catalyst.
  • Examples of a granulation method used herein include a stirring granulation method, a spraying granulation method, a tumbling granulation method, a bricketing granulation method, a compacting granulation method, an extruding granulation method, a fluidized layer granulation method, an emulsifying granulation method, a suspending granulation method a press-molding granulation method, and the like, but the granulation method is not limited thereto.
  • Preferable examples include a stirring granulation method, a spraying granulation method, a tumbling granulation method and a fluidizing granulation method, and particularly preferable examples include a stirring granulation method and a spraying granulation method.
  • examples of a dispersion medium used for a starting slurry include water or an organic solvent.
  • water is used as a dispersion medium.
  • a concentration of the ion-exchange layered silicate in a starting material slurry for the spraying granulation method producing spherical particles is from 0.1 to 70%, preferably from 1 to 50 wt%, more preferably from 5 to 30 wt%, based upon the weight of the slurry.
  • An entrance temperature of hot air used in the spraying granulation method producing sphere particles varies depending on a dispersion medium used, but it is typically 120 to 600°C, preferably 150 to 590°C, when water is used as a dispersion medium.
  • the outlet temperature is from 80 to 260°C, preferably 100 to 200°C, preferably 120 to 180°C.
  • an organic material an inorganic solvent, an inorganic salt, various binders, and the like, may be used.
  • the binders include sugar, dextrose, corn syrup, gelatin, glue, carboxymethylcelluloses, polyvinyl alcohol, water- glass, magnesium chloride, aluminum sulfate, aluminum chloride, magnesium sulfate, alcohols, glycol, starch, casein, latex, polyethylene glycol, polyethylene oxide, tar, pitch, alumina sol, gum arabic, sodium alginate, and the like.
  • the pulverizing method is not specially limited, and it may be either dry type pulverization or wet type pulverization.
  • the agglomerates When the agglomerates are formed by spray drying, they can be further characterized in that typically at least 80, preferably at least 90, and most preferably at least 95 volume % of that fraction of the support agglomerate particles smaller that the D90 of the entire agglomerate particle size distribution possesses microspheroidal shape (i.e., morphology). Evaluation of the microspheroidal morphology is performed on that fraction of the particle size distribution of the support agglomerates, which is smaller than the D90, to avoid distortion of the results by a few large particle chunks, which because of their large volume, would constitute a non-representative sample of the agglomerate volume.
  • microspheroidal shape i.e., morphology
  • spheroidal as used herein, means small particles of a generally rounded, but not necessarily spherical shape. This term is intended to distinguish from irregular jagged chunks and leaf or rod like configurations. "Spheroidal” is also intended to include polylobed configurations wherein the lobes are also generally rounded, although polylobed structures are uncommon when the agglomerate is made as described herein.
  • Each microspheroid is preferably composed of a loosely to densely packed composite of Components-A and -B typically with some, to substantially no, interstitial void spaces, and typically, substantially no visible boundaries, in an electron micrograph, between particles originally derived from Components-A and -B.
  • Spray drying conditions are typically controlled in order to impart the desired target properties described above to the agglomerate.
  • the most influential spray drying conditions are the pH of the aqueous slurry to be spray dried, as well as its dry solids content.
  • dry solids content as used herein is meant the weight of solids in the slurry after such solids have been dried at 175°C for 3 hours, and then at 955°C for 1 hour. Thus, dry solids content is used to quantify the weight of solid ingredients which exist in the slurry and to avoid inclusion of adsorbed water in such weight.
  • the pH of the slurry will be controlled or adjusted to be from about 2 to about 10 (e.g., 3 to 9, preferably from about 7 to about 9, such as about 4, and the dry solids content will be controlled or adjusted to be typically from about 10 to 40, preferably from 10 to 30, preferably from about 15 to about 25, and most preferably from about 18 to about 22 (e.g., 20) wt% based on the weight of the slurry and the dry weight of the gel.
  • the pH of the slurry will be controlled or adjusted to be from about 2 to about 10 (e.g., 3 to 9, preferably from about 7 to about 9, such as about 4, and the dry solids content will be controlled or adjusted to be typically from about 10 to 40, preferably from 10 to 30, preferably from about 15 to about 25, and most preferably from about 18 to about 22 (e.g., 20) wt% based on the weight of the slurry and the dry weight of the gel.
  • Control of the remaining variables in the spray drying process such as the viscosity and temperature of the feed, surface tension of the feed, feed rate, the selection and operation of the atomizer (preferably an air atomizer is employed and, optionally, with the use of a pressure nozzle, the atomization energy applied, the manner in which air and spray are contacted, and the rate of drying, are well within the skill of the spray dry artisan once directed by the target properties sought to be imparted to the product produced by the spray drying. (See, for example, US 4,131,452.)
  • the pH of the slurry will be controlled or adjusted to be from about 3 to 7; the dry solids content will be controlled or adjusted to be typically from about 20 to 30 wt% based on the weight of the slurry and the dry weight of the gel; and the ratio of Component-A to Component-B will be in the range of 1 :5 to 1 :20.
  • the pH of the slurry will be controlled or adjusted to be from about 3 to 7; the dry solids content will be controlled or adjusted to be typically from about 20 to 30 wt% based on the weight of the slurry and the dry weight of the gel; and the ratio of Component-A to Component-B will be in the range of 1 :5 to 1 :20 and a spray dried material having an average particle size of from 20 to 125 is obtained, preferably the particle is free flowing.
  • Product separation from the drying air follows completion of the spray drying stage when the dried product remains suspended in the air. Any convenient collection method can be employed, such as removal from the base of the spray dryer by the use of separation equipment.
  • calcination When calcination is employed, it will typically be conducted at sufficient temperature and time to reduce the total volatiles to between about 0.1 and 8 wt.% where the total volatiles are determined by measuring the weight loss upon destructive calcination of the sample at 1000°C.
  • the calcination temperature will also affect the interrelationship between the desired silica:clay ratio and the organoaluminum compound amount, and the activity of the catalyst as described hereinafter in more detail.
  • calcination when employed, will typically be conducted by heating the support to temperatures of typically from about 100 to about 800, preferably from about 150 to about 600, and most preferably from about 200 to about 300°C for periods of typically from about 1 to about 600 (e.g., 50 to 600), and preferably from about 50 to about 300 minutes.
  • the atmosphere of calcination can be air or an inert gas. Calcination should be conducted to avoid sintering.
  • the chemical treatment of an ion-exchange layered silicate is carried out by bringing it in contact with an acid, a salt, an alkali, an oxidizing agent, a reducing agent or a treating agent containing a compound intercalatable between layers of an ion-exchange layered silicate.
  • the intercalation means to introduce other material between layers of a layered material, and the material to be introduced is called a guest.
  • acid treatment or salt treatment is particularly preferable.
  • a common effect achieved by chemical treatment is to exchange an intercalation cation with other cations, and in addition to this effect, the following various effects can be achieved by various chemical treatments.
  • acid treatment removes impurities on the surface of silicate, and cations such as Al, Fe, Mg, or the like, in a crystal structure are eluted, thereby increasing the surface area. This treatment enhances the acid strength and acidity of the layered silicate.
  • Alkali treatment destroys a crystal structure of a clay mineral and changes a structure of the clay mineral.
  • intercalation or salt treatment forms an ion composite, a molecule composite, an organic derivative, or the like, and changes a surface area or a distance between layers.
  • an exchangeable intercalated cation between layers can be replaced by other large bulky ions, thereby producing a layered material having the distance between layers enlarged.
  • the bulky ions have a function as a column supporting the layered structure, and are called pillars.
  • treating agents are illustrated below.
  • at least two kinds of members selected from the group consisting of acids, salts, alkalis, oxidizing agents, reducing agents and compounds intercalatable between layers of an ion-exchange layered silicate may be combined and used as treating agents.
  • acids, salts, alkalis, oxidizing agents, reducing agents and compounds intercalatable between layers of an ion- exchange layered silicate may be respectively used in a combination of two or more members.
  • a combination of a salt treatment and an acid treatment is particularly preferable.
  • acids useful in acid treatment include hydrochloric acid, nitric acid, sulfuric acid, phosphoric acid, acetic acid, oxalic acid, and the like. Particularly, it is preferable to use an inorganic acid. Usually, the acid is used in the form of an acid aqueous solution. The acid used in the treatment may be a mixture of at least two kinds of acids. Usefully, the acid used herein is sulfuric acid.
  • Examples of salts include salts formed from a cation selected from the group consisting of an organic cation, an inorganic cation and a metal ion and anion selected from the group consisting of an organic anion, an inorganic anion, and a halide ion.
  • preferable examples include compounds formed from a cation including at least one kind of atom selected from Group 1 to Group 14 of the Periodic Table of the Elements and at least one kind of an anion selected form an anion of halogen and an anion of an inorganic Bronsted acid and an organic Bronsted acid.
  • Particularly preferable examples include compounds formed from an anion selected from the group consisting of an anion of halogen and an anion of an inorganic Bronsted acid.
  • Non-limiting examples of these salts include: LiCl, LiBr, Li 2 S0 4 , Li 3 (P0 4 ), L1NO 3 , Li(OOCCH 3 ), NaCl, NaBr, Na 2 S0 4 , Na 3 (P0 4 ), NaN0 3 , Na(OOCCH 3 ), KC1, KBr, K 2 S0 4 , K 3 (P0 4 ), KN0 3 , K(OOCCH 3 ), MgCl 2 , MgS0 4 , Mg(N0 3 ) 2 , CaCl 2 , CaS0 4 , Ca(N0 3 ) 2 , Ca 3 (C 6 H 5 0 7 ) 2 , Sc(OOCCH 3 ) 2 , Sc 2 (C0 3 ) 3 , Sc 2 (C 2 0 4 ) 3 , Sc(N0 3 ) 3 , Sc 2 (S0 4 ) 3 , ScF 3 , ScCl 3 , ScB
  • Examples of an organic cation include an ammonium compound such as tetraethylammonium, tetramethylammonium, benzyltrimethylammonium, trimethylammonium, triethylammonium, tripropylammonium, tributylammonium, dodecylammonium, N,N-dimethylanilinium, ⁇ , ⁇ -diethylanilinium, N,N-2,4,5- pentamethylanilinium, ⁇ , ⁇ -dimethyloctadecylammonium, octadecylammonium, N,N- dimethyl-p-n-butylanilinium, N,N-dimethyl-p-trimethylsilylanilinium, ⁇ , ⁇ -dimethyl- 1 - napthylanilinium, ⁇ , ⁇ -2-trimethylanilinium, 2,6-dimethylanilinium, or the like, a nitrogen- containing aromatic compound such as t
  • the ion-exchange layered silicate has been treated with one or more of tetraethylammonium, tetramethylammonium, benzyltrimethylammonium, trimethylammonium, triethylammonium, tripropylammonium, tributylammonium, dodecylammonium, N,N-dimethylanilinium, ⁇ , ⁇ -diethylanilinium, N,N-2,4,5- pentamethylanilinium, ⁇ , ⁇ -dimethyloctadecylammonium, octadecylammonium, N,N- dimethyl-p-n-butylanilinium, N,N-dimethyl-p-trimethylsilylanilinium, N,N-dimethyl- 1 - napthylanilinium, ⁇ , ⁇ -2-trimethylanilinium, 2,6-dimethylanilinium, pyridin
  • examples of other anions include an anion of a boron compound or a phosphorus compound such as hexafluorophosphate, tetrafluoroborate, tetraphenylborate, or the like, but the anion is not limited thereto.
  • These salts may be used alone or in a mixture of two or more. Further, they may be used in combination with acids, alkalis, oxidizing agents, reducing agents, compounds intercalatable between layers of an ion-exchange layered silicate, or the like. They may be combined with a treating agent to be added to the initiation or treatment, or they may be combined with a treating agent to be added during treatment.
  • Examples of a treating agent used in alkali treatment include LiOH, NaOH, KOH, Mg(OH) 2 , Ca(OH) 2 , Sr(OH) 2 , Ba(OH) 2 , and the like. Since it is considered that the alkali treatment may damage the acidity of an ion-exchanged layered silicate, it is preferable to carry out acid treatment after achieving a structure change of a clay mineral by alkali treatment. However, even after the alkali treatment, if an acidity and an acid amount satisfy the above mentioned ranges, the effect of the present invention is not damaged.
  • Examples of a preferable compound include LiOH, NaOH, KOH, Mg(OH) 2 , or the like.
  • Examples of an oxidizing agent include permanganates such as HMn0 4 , NaMn0 4 , KMn0 4 or the like, nitric acid compounds such as HN0 3 , N 2 0 4 , N 2 0, Cu(N0 3 ) 2 , Pb(N0 3 ) 2 , AgN0 3 , KNO 3 , NH 4 N0 3 , or the like, halogens such as F 2 , Cl 2 , Br 2 , or I 2 , peroxides such as H 2 0 2 , Na 2 0 2 , Ba0 2 , (C 6 H 5 CO) 2 0 2 , K 2 S 2 08, K 2 S0 5 , HCO3H, CH3CO3H, C 6 H 5 C0 3 H, C 6 H 4 (COOH)C0 3 H, CF 3 CO 3 H or the like, oxyacids such as KIO, KCIO, KBrO, KCIO 3 , KBr0
  • Examples of a reducing agent include hydrogen and hydrogen compounds such as H 2 , HI, H 2 S, LiAlH 4 , NaBH 4 , or the like, sulfur compounds such as S0 2 , Na 2 S, or the like, alkali metals, alkaline earth metals, metals of Group 3 to Group 10 of the Periodic Table of the Elements or their alloys, metal salts of a low atomic valence state such as Fe(II), Sn(II), ⁇ ( ⁇ ), Cr(n), or the like, CO, and the like.
  • hydrogen and hydrogen compounds such as H 2 , HI, H 2 S, LiAlH 4 , NaBH 4 , or the like
  • sulfur compounds such as S0 2 , Na 2 S, or the like
  • alkali metals alkaline earth metals
  • metals of Group 3 to Group 10 of the Periodic Table of the Elements or their alloys metal salts of a low atomic valence state such as Fe(II), Sn(II), ⁇
  • Examples of a guest compound intercalated into layers of an ion-exchange layered silicate include a cationic inorganic compound such as TiCl 4 , ZrCl 4 , or the like, a metal alcoholate such as Ti(OR) 4 , Zr(OR) 4 , PO(OR)3, B(OR)3, (R is an alkyl group or an aryl group) or the like, a metal hydroxide or carboxylate ion such as [Ali 3 0 4 (OH)2 4 ]7 + , [Zr 4 (OH)i 4 ]2 + , [Fe 3 0(OCOCH 3 )6] + , or the like, an organic compound such as ethylene glycol, glycerol, urea, hydrazine, or the like, and an organic cation such as an alkyl ammonium ion, or the like.
  • a cationic inorganic compound such as TiCl 4 , ZrCl 4 , or
  • a polymerized material obtained by hydrolyzing a metal alcoholate such as Si(OR) 4 , Al(OR)3, Ge(OR) 4 , or the like, or a colloidal inorganic compound such as S1O2, or the like may also be present.
  • a pillar include an oxide, or the like, formed by intercalating the above hydroxide ion between layers and then dehydrating by heat.
  • a guest compound may be used as it is or may be used after newly adsorbing water or after heat-dehydrating. Also, the guest compound may be used alone or in a mixture of two or more of the above solids.
  • the above-mentioned various treating agents may be used as a treating agent solution by dissolving in an appropriate solvent, or it is possible to use a treating agent itself as a solvent.
  • a usable solvent include water, alcohols, aliphatic hydrocarbons, aromatic hydrocarbons, esters, ethers, ketones, aldehydes, furans, amines, dime thylsulf oxide, dimethylformamide, carbon disulfide, nitrobenzene, pyridines, or their halides.
  • a concentration of a treating agent in a treating agent solution is preferably from 0.1 to 100 wt%, more preferably from 5 to 50 wt.%. If the treating agent concentration is within these ranges, a time required for treatment becomes shorter and an efficient production is possible.
  • An acid treatment removes impurities on the surface or ion-exchanges a cation present between layers, and in addition to this function, the acid treatment elutes a part or whole of cations such as Al, Fe, Mg, or the like, in a crystal structure.
  • acids used in acid treatment include hydrochloric acid, nitric acid, sulfuric acid, phosphoric acid, acetic acid, oxalic acid, and the like. Particularly, it is preferable to use an inorganic acid.
  • the acid is typically used in the form of an acid aqueous solution.
  • the acid used in the treatment may be a mixture of at least two kinds of acids.
  • the acid used herein is sulfuric acid.
  • a particular embodiment of the present invention is to carry out a treatment with an acid having a specific concentration. Any concentration of acid may be used, however higher acid concentrations (and higher temperatures) are more efficient. In particular using an acid concentration of more than 5 wt% (based upon the weight of the acid, any liquid diluent or solvent and the ion exchange layered silicate present), preferably more than 10 wt%, more preferably more than 15 wt% has been found to be effective.
  • the treatment is performed at temperatures of more than 50°C, preferably more than 70°C, more preferably at more than 90°C.
  • the treatment preferably is allowed to react for 5 minutes to 10 hours, more preferably 30 minutes to 8 hours, more preferably 1 to 6 hours.
  • the treatment occurs at 90°C or more for 2 to 6 hours using an acid concentration of more than 15 wt%. In another particularly preferred embodiment, the treatment occurs at 100°C or more for 2 to 4 hours using an acid concentration of more than 15 wt%.
  • a silicate treated by an acid having a high concentration provides a larger pore size, and it is expected that mass transport (of a metallocene complex, a monomer, an organoaluminum compound, a heterocyclic organic compound or the like) becomes easy in the inside of a catalyst or constituting particles in the same manner as in the outside. Accordingly, a catalyst prepared from the silicate of the present invention has active sites more uniformly dispersed, and it is considered that local heat generation on the catalyst is inhibited as compared with a conventional catalyst.
  • the ion-exchange layered silicate will, preferably, have a surface area in the range of 100 to 450 m 2 /g, preferably 150 to 400 m 2 /g, more preferably 200 to 350 m 2 /g.
  • An acid used for the concentrated acid treatment may be the same as those used in an ordinary acid treatment, but is preferably sulfuric acid, nitric acid or hydrochloric acid more preferably sulfuric acid.
  • the salt treatment means a treatment carried out for the purpose of exchanging cations in an ion- exchange layered silicate.
  • the treating conditions with a salt are not specially limited, but it is preferable to carry out the salt treatment under conditions of a salt concentration of from 0.1 to 50 wt%, a treating temperature of from room temperature to a boiling point and a treating time of from 5 minutes to 24 hours in such a manner as to elute at least a part of the materials constituting an ion-exchange layered silicate.
  • the salt may be used in an organic solvent such as toluene, n-heptane, ethanol, or the like, or may be used in the absence of a solvent if it is liquid-like at the treating temperature, but it is, preferably, used as an aqueous solution.
  • an organic solvent such as toluene, n-heptane, ethanol, or the like
  • the salt treatment achieves an effect similar to an acid treatment.
  • ion exchange at least 40%, preferably at least 60% of ion exchangeable cations of Group 1 metals contained in an ion-exchange layered silicate with cations dissociated from the salts as described above.
  • ion exchangeable cations of Group 1 metals contained in an ion-exchange layered silicate with cations dissociated from the salts as described above it is preferable to remove ions eluted from the treatment and an excess amount of a treating agent.
  • water or an organic solvent is generally used.
  • drying is carried out generally at a drying temperature of from 100 to 800°C, preferably from 150 to 600°C.
  • ion-exchange layered silicates change their properties depending on a drying temperature employed even when their structures are not destroyed, and it is, therefore, preferable to change a drying temperature depending on their uses.
  • the drying period is usually in a range of from 1 minute to 24 hours, preferably from 5 minutes to 6 hours, and a drying atmosphere is preferably dry air, dry nitrogen, dry argon, or carried out under reduced pressure.
  • a drying method is not specially limited, but various methods may be employed.
  • ion-exchange layered silicates subjected to both acid and/or salt (or a combination thereof) chemical treatments described above have one or more of the following features (as outlined in US 6,531 ,552 and US 2003/0027950), which is fully incorporated herein by reference):
  • a pore diameter D m i / 2(A) on the smaller pore size side corresponding to a 1/2 peak intensity of the maximum peak intensity DVM has a relation of Dmi / 2/ Dm of at least 0.65 and less than 1, provided that the largest value is employed when there are a plurality of D m i / 2 values, and or
  • the term "acid” used herein is one category classifying a material, and is defined as a material of Bronsted acid or Lewis acid.
  • the term "acid site” is defined as a constituting unit of a material exhibiting a property as an acid, and for the present invention, its amount is analyzed by the method described in US 6,531,552, which is fully incorporated herein by reference.
  • a chemically treated ion-exchange layered silicate is used as the support or carrier, the amount of a specific acidity is measured with regard to a silicate obtained after the chemical treatment.
  • the ion-exchange layered silicate is acidic in nature as determined by titration methods as outlined in US 6,531,552, which is fully incorporated herein by reference.
  • an acidity and amount of acid sites it is important to control an acidity and amount of acid sites, so as to afford an ion-exchange layered silicate that contains aluminum in an atomic ratio of Al/Si in a range of from 0.05 to 0.4, preferably from 0.05 to 0.25, more preferably from 0.07 to 0.23.
  • the Al/Si atomic ratio is regarded as an index of acid treatment of the clay constituent.
  • the chemically treated ion-exchange layered silicate having an acid site of at most -8.2 pKa, with the amount of acid site being equivalent to at least 0.05 mmol/g of 2,6-dimethylpyridine consumed for neutralization (as described in US 6,531,552).
  • the preferred amount of acid sites present in the ion-exchange layered silicate is 0.05 mmol/g or more and the amount of acid sites is preferably as high as possible.
  • the chemically treated ion-exchange layered silicate performance in the nitrogen adsorption-desorption isotherm exhibits a hysteresis.
  • Examples of the analyzing apparatus include commercially available products such as Autosorb of Quantachrome Company or Omnisorp of Coulter Inc., or the like.
  • the evaluation of the pore size distribution in the present invention employs the desorption isotherm.
  • the desorption isotherm is a curve obtained while reducing the relative pressure.
  • the desorption isotherm shows a lower relative pressure to the same desorbed gas amount as compared with adsorption isotherm, and, consequently, shows a lower free energy state, and is generally considered to be closer to a state of real thermodynamic stability.
  • an ion-exchange layered silicate with any pore size and or any pore size distribution may be used.
  • D m represents a pore size diameter showing a maximum peak intensity and is generally expressed as "most frequently appearing pore diameter”
  • D V M represents a maximum peak intensity
  • D ml/2 represents a pore size diameter on the smaller diameter side corresponding to a point, the peak intensity of which is 1/2 of the maximum peak intensity.
  • a pore diameter D m i/ 2 is present, at least one respectively, on both sides of D m , i.e., on the larger diameter side of D m and on the smaller diameter side of D m , but a value on the smaller diameter side is taken as the D m i/ 2 value in the present invention. Also, if there are a plurality of D m i/ 2 values on the smaller diameter side, the largest value is employed for calculation.
  • the D ml/2 /D m can range from 0.1 to 0.9.
  • a D m i/2/D m value is preferably at least 0.68, more preferably at least 0.70.
  • a pore size distribution curve calculated from desorption isotherm by the nitrogen adsorption-desorption method a pore diameter D ml/3 (A) on the smaller pore size side corresponding to a 1/3 peak intensity of the maximum peak intensity D vm has a relation of D m i 3/ D m of at least 0.55 and less than 1 , provided that the largest value is employed when there are a plurality of D ml/3 values.
  • a pore diameter D m i 3 value is present respectively on both sides of D m , i.e., at least one on the larger diameter side of D m and at least one on the smaller diameter side of D m , but a value on the smaller diameter side is defined as D ml/3 .
  • D m i /3 /D m value is, preferably, at least 0.56, more preferably at least 0.57. If the D m i /3 /D m value is less than 0.56, a considerable amount of smaller diameter pores are present, which is not preferred.
  • the pore size distribution calculated for desorption isotherm by the nitrogen adsorption-desorption method is a substantially unimodal peak. That is, there is not present a second peak, and if it is present, its intensity is at most 50%, preferably at most 40%, particularly at most 30% of a maximum peak intensity D VM -
  • the pore size distribution curve calculated from desorption isotherm by the nitrogen adsorption-desorption method wherein a peak intensity at a pore diameter of 50 A is defined as D VSOA, D VSOA D VM is at least 0.01 and at most 0.40, preferably at least 0.03 and at most 0.38, more preferably at least 0.05 and at most 0.36. If the D VSOA /D VM value exceeds 0.38, a considerable amount of smaller diameter pores are contained.
  • an ion-exchange layered silicate may have a predetermined pore size, but its pore size is sufficiently large to accept a metallocene complex, an activator, an organoaluminum compound, and a monomer. Accordingly, these compounds participating in the reaction easily enter into pores in respective stages of formation of a catalyst, activation, prepolymerization and polymerization, and complexes are highly dispersed in carriers, and consequently metallocene catalyst active sites are thought to be uniformly formed.
  • the ion exchange layered silicate has a pore size that is sufficiently large enough that the catalyst compound, the organoaluminum and activator compounds may freely enter and diffuse evenly within the particle. Preferred pore sizes include 40 Angstroms to 500 Angstroms, preferably 50 Angstroms to 300 Angstroms, more preferably 70 to 200 Angstroms.
  • the spray dried agglomerate has a compression fracture strength (also called average crushing strength) as measured by a minute compression tester.
  • the ion exchange layered silicate has a compression fracture strength of 3 to 20 MPa.
  • the average crushing strength is at least 5 MPa, more preferably at least 7 MPa.
  • the upper limit of the ion-exchange layered silicate strength is, preferably, an average crushing strength of at most 20 MPa, more preferably at most 18 MPa.
  • ion-exchange layered silicate is preferably contacted with an organoaluminum compound, optionally, before treatment with the catalyst compound(s).
  • preferred organoaluminum compounds described above are represented by the Formula:
  • each R is independently a substituted or unsubstituted alkyl group and/or a substituted or unsubstituted aryl group.
  • R is an alkyl group containing 1 to 30 carbon atoms.
  • Preferred R groups include methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, docecyl, aryl, and all isomers thereof.
  • the preferred organoaluminum compounds include alkylaluminum compounds and/or alumoxanes, preferably methylalumoxane, modified methylalumoxane, or ethylalumoxane.
  • the organoaluminum compounds include alkylaluminum compounds where the alkyl is a Ci to C 4 o linear, branched or cyclic alkyl, preferably a Ci to Ci 2 linear or branched alkyl, preferably methyl, ethyl, propyl, butyl, isobutyl, n-butyl, isopentyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl or dodecyl, even more preferably methyl, ethyl, propyl, butyl, isobutyl, n-butyl, or hexyl.
  • Preferred organoaluminum compounds include those represented by the Formula:
  • R is a hydrocarbon group having a carbon number of from 1 to 30, preferably 4 to 12
  • Y is hydrogen, halogen, an alkoxy group or a siloxy group
  • n is 1, 2, or 3.
  • Particularly preferred alkyl aluminum compounds useful in this invention include: trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, tri-iso- octylaluminum, triphenylaluminum, and combinations thereof.
  • the organoaluminum compounds also include combinations of organoaluminum compounds.
  • organoaluminum compounds such as two or more of trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, tri-iso-octylaluminum, and triphenylaluminum.
  • the organoaluminum compound comprises one or more alumoxanes, which are generally oligomeric compounds, containing -Al(R)-0- or -Al(R)2-0- subunits, where R is an alkyl group, preferably a Ci to C 4 o linear, branched or cyclic alkyl, preferably a Ci to Ci 2 linear or branched alkyl, preferably methyl, ethyl, propyl, butyl, isobutyl, n-butyl, isopentyl, pentyl, hexyl, heptyl octyl, nonyl, decyl or dodecyl, even more preferably methyl, ethyl, propyl, butyl, isobutyl, n-butyl, or hexyl.
  • R is an alkyl group, preferably a Ci to C 4 o linear, branched or cyclic alkyl,
  • alumoxanes examples include methylalumoxane (MAO), modified methylalumoxane (MMAO), ethylalumoxane, isobutylalumoxane, tetraethyldialumoxane and di-isobutylalumoxane.
  • Alumoxanes may be produced by the hydrolysis of the respective trialkylaluminum compound.
  • MMAO may be produced by the hydrolysis of trimethylaluminum and a higher trialkylaluminum such as triisobutylaluminum.
  • Contact between an ion-exchange layered silicate and an organoaluminum compound can be carried out under an inert gas atmosphere such as nitrogen in a solvent of an inert hydrocarbon such as hexane, heptane, pentane, cyclohexane, benzene, toluene, xylene, or the like, and the solvent may be used alone or in a mixture of two or more.
  • an inert gas atmosphere such as nitrogen in a solvent of an inert hydrocarbon such as hexane, heptane, pentane, cyclohexane, benzene, toluene, xylene, or the like, and the solvent may be used alone or in a mixture of two or more.
  • An amount of an organoaluminum compound used is preferably from 0.01 to 1000 mmol, more preferably from 0.1 to 100 mmol, per 1 g of an ion-exchange layered silicate.
  • a concentration of an ion-exchange layered silicate in a solvent is preferably from 0.001 to 100 g/mL, more preferably form 0.01 to 10 g/mL, and a concentration of an organoaluminum compound is preferably from 0.001 to 100 mmol/mL, more preferably from 0.01 to 10 mmol.
  • Contacting may be carried out by dispersing an ion-exchange layered silicate in a solvent and then bringing an organoaluminum compound in contact therewith.
  • contacting may be carried out by adding an organoaluminum compound to a solvent and then dispersing an ion-exchange layered silicate therein.
  • the contacting treatment is carried out generally at a temperature of from -50°C to a boiling point of a solvent, preferably from 0°C to a boiling point of a solvent.
  • the contacting time is from 1 minute to 48 hours, preferably from 1 minute to 24 hours.
  • the order of contacting an organoaluminum compound with an ion-exchange layered silicate is not specially limited as far as the object of the present invention is achieved, but it is more effective to carry out the contacting treatment after chemical treatment of the silicate or preferably after drying carried out after the chemical treatment. It is also preferable to contact the organoaluminum compound with an ion-exchange layered silicate after spray drying the aqueous mixture of ion-exchange layered silicate and inorganic oxide.
  • the order of contacting treatment step of an organoaluminum compound and an ion-exchange layered silicate and the granulation step of an ion-exchange layered silicate is not specially limited as far as the object of the present invention is achieved, but it is preferable to carry out the treatment with an organoaluminum compound after granulating the silicate.
  • a carrier obtained through the following Step 1 and Step 2 is used as a catalyst component for olefin polymerization.
  • Step 1 after granulating an ion-exchange layered silicate, the silicate is treated with an acid having an acid concentration as described above and is then contacted with an inorganic oxide and thereafter spray dried.
  • Step 2 after carrying out step 1, the silicate-inorganic oxide particle is treated with an organoaluminum compound, which is any organoaluminum compound from the discussion above.
  • organoaluminum compound which is any organoaluminum compound from the discussion above.
  • Preferred treated organoaluminum layered silicates include: triethyaluminum treated montmorillonite, triisobutylaluminum treated montmorillonite, triethylaluminum treated montmorillonite/silicate, preferably where the montmorillonite/silicate is spray dried, tri-n-octylaluminum treated monmorillonite-silicate, preferably where the montmorillonite/silicate is spray dried, trimethylaluminum treated montmorillonite-silicate, preferably where the montmorillonite/silicate is spray dried, and the like.
  • activator is used herein to be any compound which can activate any one of the catalyst compounds described above by converting the neutral catalyst compound to a catalytically active metallocene compound cation.
  • the organoaluminum treated layered silicates alone or in combination with inorganic oxides described herein function as an activator and thus allow polymerization without the use of traditional activators such as alumoxanes or non-coordinating anions. While traditional activators can also be used, it is useful if traditional activators are not present or if present are present at a ratio of activator metal (such as Al or B) to catalyst transition metal of less than 1 : 1 , preferably less than 0.5 to 1 , preferably less than 0.1 : 1.
  • Alumoxanes are generally oligomeric compounds containing -Al(Rl)-0- sub- units, where Rl is an alkyl group.
  • alumoxanes include methylalumoxane (MAO), modified methylalumoxane (MMAO), ethylalumoxane, isobutylalumoxane, and mixtures thereof.
  • Alkylalumoxanes and modified alkylalumoxanes are suitable as catalyst activators, particularly when the abstractable ligand is an alkyl, halide, alkoxide, or amide. Mixtures of different alumoxanes and modified alumoxanes may also be used.
  • a visually clear methylalumoxane A cloudy or gelled alumoxane can be filtered to produce a clear solution or clear alumoxane can be decanted from the cloudy solution.
  • Another useful alumoxane is a modified methylalumoxane (MMAO) cocatalyst type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylalumoxane type 3 A, covered under US 5,041,584).
  • MMAO modified methylalumoxane
  • the activator is an alkylalumoxane, preferably methylalumoxane or isobutylalumoxane.
  • alumoxane is not present, or if present is present at an aluminum to transition metal ratio of less than 10: 1, preferably 1 :0, preferably less than 0.1 : 1.
  • the catalyst system of this invention further comprises one or more stoichiometric activators.
  • a stoichiometric activator is a non-alumoxane compound which when combined in a reaction with the metallocene compound forms a catalytically active species at a molar ratio of stoichiometric activator to metallocene compound of 10: 1 or less (preferably 5: 1, more preferably 2: 1, or even more preferably 1 : 1), such as a compound comprising a non-coordinating anion.
  • a stoichiometric activator is not present, or if present is present at a molar ratio of stoichiometric activator to catalyst compound of less than less than 1 : 1, preferably 0.1 : 1, preferably less than 0.01 : 1.
  • Stoichiometric activators may comprise an anion, preferably a non-coordinating anion.
  • non-coordinating anion means an anion which either does not coordinate to said cation or which is only weakly coordinated to said cation thereby remaining sufficiently labile to be displaced by a neutral Lewis base.
  • “Compatible” non-coordinating anions are those which are not degraded to neutrality when the initially formed complex decomposes. Further, the anion will not transfer an anionic substituent or fragment to the cation so as to cause it to form a neutral four coordinate metallocene compound and a neutral by-product from the anion.
  • Non-coordinating anions useful in accordance with this invention are those that are compatible, stabilize the metallocene cation in the sense of balancing its ionic charge at +1 , yet retain sufficient lability to permit displacement by an ethylenically or acetylenically unsaturated monomer during polymerization.
  • ( ⁇ ) ⁇ + is the cation component and A ⁇ - is the anion component;
  • Z is (L-H) or a reducible Lewis Acid, L is a neutral Lewis base; H is hydrogen; (L-H) + is a Bronsted acid; Ad- is a non-coordinating anion having the charge d-; and d is an integer from 1 to 3.
  • the cation component may include Bronsted acids such as protonated Lewis bases capable of protonating a moiety, such as an alkyl or aryl, from the bulky ligand metallocene-containing transition metal catalyst precursor, resulting in a cationic transition metal species.
  • Bronsted acids such as protonated Lewis bases capable of protonating a moiety, such as an alkyl or aryl, from the bulky ligand metallocene-containing transition metal catalyst precursor, resulting in a cationic transition metal species.
  • the activating cation (L- ⁇ ) ⁇ "1" is a Bronsted acid, capable of donating a proton to the transition metal catalytic precursor resulting in a transition metal cation, including ammoniums, oxoniums, phosphoniums, silyliums, and mixtures thereof, preferably ammoniums of methylamine, aniline, dimethylamine, diethylamine, N-methylaniline, diphenylamine, trimethylamine, triethylamine, ⁇ , ⁇ -dimethylaniline, methyldiphenylamine, pyridine, p-bromo ⁇ , ⁇ -dimethylaniline, p-nitro-N,N-dimethylaniline, phosphoniums from triethylphosphine, triphenylphosphine, and diphenylphosphine, oxoniums from ethers, such as dimethyl ether diethyl ether, tetrahydrofuran, and
  • ( ⁇ ) ⁇ + is preferably represented by the formula: (Ar3C) + , where Ar is aryl or aryl substituted with a heteroatom, a CI to C40 hydrocarbyl, or a substituted CI to C40 hydrocarbyl, preferably (Z)d + is represented by the formula: (Ph3C) + , where Ph is phenyl or phenyl substituted with a heteroatom, a CI to C40 hydrocarbyl, or a substituted CI to C40 hydrocarbyl.
  • the reducible Lewis acid is triphenyl carbenium.
  • each Q is a fluorinated hydrocarbyl group having 1 to 20 carbon atoms, more preferably each Q is a fluorinated aryl group, and most preferably each Q is a pentafluoryl aryl group.
  • suitable A ⁇ - components also include diboron compounds as disclosed in US 5,447,895, which is fully incorporated herein by reference.
  • the ionic stoichiometric activator may be an activator comprising expanded anions, represented by the Formula:
  • A* is a cation having charge +a;
  • Z* is an anion group of from 1 to 50 atoms not counting hydrogen atoms, further containing two or more Lewis base sites;
  • J* independently each occurrence is a Lewis acid coordinated to at least one Lewis base site of Z*, and, optionally, two or more such J* groups may be joined together in a moiety having multiple Lewis acid functionality;
  • J is a number from 2 to 12; and a, b, c, and d are integers from 1 to 3, with the proviso that a x b is equal to c x d.
  • Examples of such activators comprising expandable anions may be found in US 6,395,671, which is fully incorporated herein by reference.
  • cocatalysts may be used.
  • Aluminum alkyl or organometallic compounds which may be utilized as cocatalysts (or scavengers) include, for example, triethylaluminum, tri-isobutylaluminum, tri-n- hexylaluminum, tri-n-octylaluminum, diethyl aluminum chloride, dibutyl zinc, diethyl zinc, and the like.
  • cocatalyst is present at a molar ratio of cocatalyst metal to transition metal of less than 100: 1 , preferably less than 50: 1, preferably less than 15: 1 , preferably less than 10: 1. In alternate embodiments, the cocatalyst is present at 0 wt%.
  • additives may also be used, as desired, such as one or more scavengers, promoters, modifiers, reducing agents, oxidizing agents, aluminum alkyls, or silanes.
  • any method of combining the catalyst compound and support may be used.
  • the support material is slurried in a non-polar solvent and the resulting slurry is contacted with a solution of a catalyst.
  • the slurry mixture may be heated to 0°C to 70°C, preferably to 25°C to 60°C, preferably at room temperature (25 °C).
  • Contact times typically range from 0.5 hour to 24 hours, from 2 hours to 16 hours, or from 4 hours to 8 hours.
  • Suitable non-polar solvents are materials in which all of the reagents used herein, i.e., the activator, and the catalyst compound, are at least partially soluble and which are liquid at reaction temperatures.
  • Preferred non-polar solvents are alkanes, such as isopentane, hexane, n-heptane, octane, nonane, and decane, although a variety of other materials including cycloalkanes, such as cyclohexane, aromatics, such as benzene, toluene, and ethylbenzene, alone or in combination, may also be employed.
  • the weight ratio of the catalyst to the solid support material may be from 10: 1 to 0.0001 : 1, from 1 : 1 to 0.001 : 1 , or from 0.1 : 1 to 0.001 : 1.
  • the weight ratio of the support material to the activator compound (such as an alumoxane) may range from 1 : 10 to 100: 1 , from 1 : 1 to 100: 1, or from 1 : 1 to 10: 1.
  • the supported catalyst system is suspended in a paraffinic agent, such as mineral oil, for easy addition to a reactor system, for example a gas phase polymerization system.
  • a paraffinic agent such as mineral oil
  • This invention also relates to polymerization processes comprising: contacting one or more olefins with the catalyst system of the present invention under polymerization conditions; and obtaining an olefin polymer.
  • the catalyst systems described herein are useful in the polymerization of all types of olefins. This includes polymerization processes which produce homopolymers, copolymers, terpolymers, and the like, as well as block copolymers and impact copolymers.
  • Monomers useful herein include substituted or unsubstituted C2 to C40 olefins, preferably C2 to C20 olefins, preferably C2 to C ⁇ 2 olefins, preferably ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, and isomers thereof, preferably alpha olefins.
  • the monomer comprises propylene and optional comonomers comprising one or more ethylene or C4 to C40 olefins, preferably C4 to C20 olefins, or preferably C5 to C ⁇ 2 olefins.
  • the C4 to C40 olefin monomers may be linear, branched, or cyclic.
  • the C4 to C40 cyclic olefins may be strained or unstrained, monocyclic or polycyclic, and may optionally include heteroatoms and/or one or more functional groups.
  • the monomer comprises ethylene and optional comonomers comprising one or more C3 to C40 olefins, preferably C4 to C20 olefins, or preferably C5 to C ⁇ 2 olefins.
  • the C3 to C40 olefin monomers may be linear, branched, or cyclic.
  • the C3 to C40 cyclic olefins may be strained or unstrained, monocyclic or polycyclic, and may optionally include heteroatoms and/or one or more functional groups.
  • C2 to C40 olefin monomers and optional comonomers include ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, norbornene, norbomadiene, dicyclopentadiene, cyclopentene, cycloheptene, cyclooctene, cyclooctadiene, cyclododecene, 7-oxanorbornene, 7-oxanorbornadiene, substituted derivatives thereof, and isomers thereof, preferably hexene, heptene, octene, nonene, decene, dodecene, cyclooctene, 1 ,5-cyclooctadiene, l-hydroxy-4-cyclooctene, 1- acetoxy-4-cyclooctene
  • the polymerization or co-polymerization is carried out using olefins such as ethylene, propylene, 1 -butene, 1 -hexene, 4-methyl-l-pentene, and 1-octene, vinylcyclohexane, norbornene, and norbomadiene.
  • olefins such as ethylene, propylene, 1 -butene, 1 -hexene, 4-methyl-l-pentene, and 1-octene, vinylcyclohexane, norbornene, and norbomadiene.
  • propylene and ethylene are polymerized.
  • the butene source may be a mixed butene stream comprising various isomers of butene.
  • the 1 -butene monomers are expected to be preferentially consumed by the polymerization process.
  • Use of such mixed butene streams will provide an economic benefit, as these mixed streams are often waste streams from refining processes, for example, C4 raffinate streams, and can therefore be substantially less expensive than pure 1 -butene.
  • Polymerization processes of this invention can be carried out in any manner known in the art, in slurry, in suspension or in the gas phase, continuously or batchwise, or any combination thereof, in one or more steps. Slurry, and gas phase processes are preferred. A bulk homogeneous process is also useful. (A bulk process is defined to be a process where monomer concentration in all feeds to the reactor is 70 vol% or more.) Alternately, no solvent or diluent is present or added in the reaction medium (except for the small amounts used as the carrier for the catalyst system or other additives, or amounts typically found with the monomer; e.g., propane in propylene). In another embodiment, the process is a slurry process.
  • slurry polymerization process means a polymerization process where a supported catalyst is employed and monomers are polymerized on the supported catalyst particles and at least 95 wt% of polymer products derived from the supported catalyst are in granular form as solid particles (not dissolved in the diluent).
  • a gaseous stream containing one or more monomers is continuously cycled through a fluidized bed in the presence of a catalyst under reactive conditions.
  • the gaseous stream is withdrawn from the fluidized bed and recycled back into the reactor.
  • polymer product is withdrawn from the reactor and fresh monomer is added to replace the polymerized monomer.
  • any catalyst/support combination described herein is used in the gas phase to produce olefin polymer, preferably an ethylene polymer.
  • a slurry polymerization process generally operates between 1 to about 50 atmosphere pressure range (15 psi to 735 psi, 103 kPa to 5068 kPa) or even greater and temperatures in the range of 0°C to about 120°C.
  • a suspension of solid, particulate polymer is formed in a liquid polymerization diluent medium to which monomer and comonomers along with catalyst are added.
  • the suspension including diluent is 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 is typically an alkane having from 3 to 7 carbon atoms, preferably 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 must be operated above the reaction diluent critical temperature and pressure. Preferably, a hexane or an isobutane medium is employed.
  • a preferred polymerization technique useful in the invention is referred to as a particle form polymerization, or a slurry process where the temperature is kept below the temperature at which the polymer goes into solution.
  • a particle form polymerization or a slurry process where the temperature is kept below the temperature at which the polymer goes into solution.
  • the preferred temperature in the particle form process is within the range of about 85°C to about 110°C.
  • Two preferred polymerization methods for the slurry process are those employing a loop reactor and those utilizing a plurality of stirred reactors in series, parallel, or combinations thereof.
  • Non-limiting examples of slurry processes include continuous loop or stirred tank processes.
  • other examples of slurry processes are described in US 4,613,484, which is fully incorporated herein by reference.
  • the slurry process is carried out continuously in a loop reactor.
  • the catalyst as a slurry in isobutane or as a dry free flowing powder, is injected regularly to the reactor loop, which is itself filled with circulating slurry of growing polymer particles in a diluent of isobutane containing monomer and comonomer.
  • Hydrogen optionally, may be added as a molecular weight control. (In one embodiment 500 ppm or less of hydrogen is added, or 400 ppm or less or 300 ppm or less. In other embodiments at least 50 ppm of hydrogen is added, or 100 ppm or more, or 150 ppm or more.)
  • the reactor may be maintained at a pressure of 3620 kPa to 4309 kPa and at a temperature in the range of about 60°C to about 104°C depending on the desired polymer melting characteristics. Reaction heat is removed through the loop wall since much of the reactor is in the form of a double-jacketed pipe.
  • the slurry is allowed to exit the reactor at regular intervals or continuously to a heated low pressure flash vessel, rotary dryer and a nitrogen purge column in sequence for removal of the isobutane diluent and all unreacted monomer and comonomers.
  • the resulting hydrocarbon free powder is then compounded for use in various applications.
  • additives may also be used in the polymerization, as desired, such as one or more scavengers, promoters, modifiers, chain transfer agents (such as diethyl zinc), reducing agents, oxidizing agents, hydrogen, aluminum alkyls, or silanes.
  • Useful chain transfer agents are typically alkylalumoxanes, a compound represented by the formula AIR 3 , ZnR 2 (where each R is, independently, a Ci to Cs aliphatic radical, preferably methyl, ethyl, propyl, butyl, penyl, hexyl, heptyl, octyl, or an isomer thereof) or a combination thereof, such as diethyl zinc, methylalumoxane, trimethylaluminum, triisobutylaluminum, trioctylaluminum, or a combination thereof.
  • Preferred polymerizations can be run at any temperature and/or pressure suitable to obtain the desired polymers.
  • Typical temperatures and/or pressures include a temperature greater than 30°C, preferably greater than 50°C, preferably greater than 65°C, alternately less than 200°C, preferably less than 150°C, most preferably less than 140°C, and at a pressure in the range of from 0.35 MPa to 10 MPa, preferably from 0.45 MPa to 6 MPa, or preferably from 0.5 MPa to 4 MPa.
  • the run time of the reaction is up to 300 minutes, preferably in the range of from 5 to 250 minutes, or preferably from 10 to 120 minutes.
  • hydrogen is added as a molecular-weight regulator and/or in order to increase the activity.
  • the overall pressure in the polymerization system usually is at least 0.5 bar, preferably at least 2 bar, most preferred at least 5 bar. Pressures higher than 100 bar, e.g., higher than 80 bar and, in particular, higher than 64 bar, are usually not preferred.
  • hydrogen is present in the polymerization reactor at a partial pressure of from 0.001 to 100 psig (0.007 to 690 kPa), preferably from 0.001 to 50 psig (0.007 to 345 kPa), preferably from 0.01 to 25 psig (0.07 to 172 kPa), more preferably 0.1 to 10 psig (0.7 to 70 kPa).
  • the productivity of the catalyst is at least 50 gpolymer/g (cat)/hour, preferably 500 or more gpolymer/g (cat)/hour, preferably 5000 or more gpolymer/g (cat)/hour, preferably 50,000 or more gpolymer/g (cat)/hour.
  • the conversion of olefin monomer is at least 10%, based upon polymer yield and the weight of the monomer entering the reaction zone, preferably 20% or more, preferably 30% or more, preferably 50% or more, preferably 80% or more.
  • a "reaction zone”, also referred to as a "polymerization zone”, is a vessel where polymerization takes place, for example, a batch reactor. When multiple reactors are used in either series or parallel configuration, each reactor is considered as a separate polymerization zone. For a multi-stage polymerization in both a batch reactor and a continuous reactor, each polymerization stage is considered as a separate polymerization zone. In preferred embodiments, the polymerization occurs in one, two, three, four, or more reaction zones.
  • the catalyst system used in the polymerization comprises no more than one catalyst compound.
  • additives may also be used in the polymerization, as desired, such as one or more scavengers, promoters, modifiers, chain transfer agents (such as diethyl zinc), reducing agents, oxidizing agents, hydrogen, aluminum alkyls, or silanes.
  • This invention also relates to polyolefins produced using the supported catalyst systems of this invention, particularly propylene and ethylene homopolymers and copolymers.
  • the invention relates to polyolefins produced using the catalyst systems of this invention, particularly polyethylene, having a density in the range of 0.916 to 0.955 g/cc, preferably in the range of from 0.920 to 0.950 g/cc, preferably 0.920 to 0.940 g/cc, preferably 0.920 to 0.935 g/cc.
  • SAXS/MAXS/WAXS measurements are performed using a SAXSLAB Ganesha 300XL.
  • the wavelength of the incident X-rays is 1.54 A using a micro-focus sealed CuKa source.
  • the X-rays are focused using a Silicon crystal monochromator and beam size defined by a series of vertical and horizontal slits. This slit configuration defines a beam size of approximately 0.3 mm on the sample.
  • the scattered X-rays are collected on a vacuum compatible Dectris Pilatus 300K 2D area detector. A pin diode measured the intensity after the sample and automatic corrections for sample transmission and beam intensity are done.
  • the detector is moved inside the vacuum tube to positions of 0.091 m, 0.441 m and 1.041 m for WAXS, MAXS and SAXS respectively. This gives a q range of 0.07 to 0.25 A "1 , corresponding to real-space dimensions of 2.2 to 897 A.
  • the estimated beam flux on the sample is 55 x 10 6 , 31 x 10 6 , and 4.5 x 10 6 photons/second for WAXS, MAXS, and SAXS configurations.
  • the resulting 2D patterns are collected and collapsed into a ID I(q) vs. q profile.
  • two, three, four, or more different layered silicate supports may be present in the support.
  • two, three, four, or more different layered silicate supports may be present in the polymer produced herein.
  • the process described herein produces propylene homopolymers or propylene copolymers, such as propylene-ethylene and/or propylene-a- olefin (preferably C2, and/or C4 to C20) copolymers (such as propylene -hexene copolymers, propylene-octene copolymers, or propylene-ethylene-hexene terpolymers) having a Mw/Mn of greater than 1 to 40 (preferably greater than 1 to 5).
  • copolymers of propylene have from 0 wt% to 25 wt% (alternately from 0.5 wt% to 20 wt%, alternately from 1 wt% to 15 wt%, preferably from 3 wt% to 10 wt%, preferably less than 1 wt%, preferably 0 wt%) of one or more of C2 or C4 to C40 olefin comonomer (preferably ethylene or C4 to C20 or C4 to C ⁇ 2 alpha olefin comonomer, preferably ethylene, butene, hexene, octene, decene, dodecene, preferably ethylene, butene, hexene, or octene).
  • C2 or C4 to C40 olefin comonomer preferably ethylene or C4 to C20 or C4 to C ⁇ 2 alpha olefin comonomer, preferably ethylene, butene
  • the process described herein produces ethylene homopolymers or copolymers, such as ethylene -propylene and/or ethylene- a-olef in (preferably C3 and/or C4 to C20) copolymers (such as ethylene-hexene copolymers, ethylene - octene copolymers, or ethylene-propylene-hexene terpolymers) having a Mw/Mn of greater than 1 to 40 (preferably greater than 1 to 5).
  • ethylene homopolymers or copolymers such as ethylene -propylene and/or ethylene- a-olef in (preferably C3 and/or C4 to C20) copolymers (such as ethylene-hexene copolymers, ethylene - octene copolymers, or ethylene-propylene-hexene terpolymers) having a Mw/Mn of greater than 1 to 40 (preferably greater than 1 to 5).
  • copolymers of ethylene have from 0 wt% to 25 wt% (alternately from 0.5 wt% to 20 wt%, alternately from 1 wt% to 15 wt%, preferably from 3 wt% to 10 wt%, preferably less than 1 wt%, preferably 0 wt%) of one or more of C3 to C40 olefin comonomer (preferably propylene or C3 to C20 or C4 to C12 alpha olefin comonomer, preferably propylene, butene, hexene, octene, decene, dodecene, preferably ethylene, butene, hexene, and octene).
  • C3 to C40 olefin comonomer preferably propylene or C3 to C20 or C4 to C12 alpha olefin comonomer, preferably propylene, butene, hexen
  • the monomer is ethylene and the comonomer is hexene, preferably from 1 to 15 mol% hexene, alternately 1 to 10 mol%.
  • the polymers produced herein have an Mw of 1,000,000 to 5,000,000 g/mol (preferably 1 ,500,000 to 4,000,000 g/mol) as measured by GPC.
  • the polymers produced herein have an Mw/Mn ("MWD” or "PDI”) of greater than 1 to 40 (alternately 1.2 to 20, alternately 2 to 10, alternately 2 to 5, alternately 2.5 to 4).
  • the polymer produced herein has a unimodal or multimodal molecular weight distribution as determined by Gel Permeation Chromotography (GPC).
  • GPC Gel Permeation Chromotography
  • unimodal is meant that the GPC trace has one peak or inflection point.
  • multimodal is meant that the GPC trace has at least two peaks or inflection points.
  • An inflection point is that point where the second derivative of the curve changes in sign (e.g., from negative to positive or vice versa).
  • GPC is performed as follows: A High Temperature Gel Permeation Chromatography (Agilent PL- 220), equipped with three in-line detectors, a differential refractive index detector (DRI), a light scattering (LS) detector, and a viscometer is used. Experimental details, including detector calibration, are described in: T. Sun, P. Brant, R. R. Chance, and W. W. Graessley, Macromolecules, Vol. 34, No. 19, pp. 6812-6820, (2001), and references therein. Three Agilent PLgel ⁇ Mixed-B LS columns are used. The nominal flow rate is 0.5 mL/min, and the nominal injection volume is 300 ⁇ .
  • the various transfer lines, columns, viscometer and differential refractometer (the DRI detector) are contained in an oven maintained at 145°C.
  • Solvent for the experiment is prepared by dissolving 6 grams of butylated hydroxytoluene as an antioxidant in 4 liters of Aldrich reagent grade 1 ,2,4-trichlorobenzene (TCB). The TCB mixture is then filtered through a 0.1 ⁇ Teflon filter. The TCB is then degassed with an online degasser before entering the GPC- 3D.
  • Polymer solutions are prepared by placing dry polymer in a glass container, adding the desired amount of TCB, then heating the mixture at 160°C with continuous shaking for about 2 hours. All quantities are measured gravimetrically.
  • the TCB densities used to express the polymer concentration in mass/volume units are 1.463 g/ml at room temperature and 1.284 g/ml at 145°C.
  • the injection concentration is from 0.5 to 2.0 mg/ml, with lower concentrations being used for higher molecular weight samples.
  • Prior to running each sample the DRI detector and the viscometer are purged. Flow rate in the apparatus is then increased to 0.5 ml/minute, and the DRI is allowed to stabilize for 8 hours before injecting the first sample.
  • the LS laser is turned on at least 1 to 1.5 hours before running the samples.
  • the concentration, c, at each point in the chromatogram is calculated from the baseline-subtracted DRI signal, 3 ⁇ 4)RI, using the following equation:
  • Kj is a constant determined by calibrating the DRI
  • (dn/dc) is the refractive index increment for the system.
  • the LS detector is a Wyatt Technology High Temperature DAWN HELEOS.
  • M molecular weight at each point in the chromatogram is determined by analyzing the LS output using the Zimm model for static light scattering (M.B. Huglin, LIGHT SCATTERING FROM POLYMER SOLUTIONS, Academic Press, 1971):
  • AR(0) is the measured excess Rayleigh scattering intensity at scattering angle ⁇
  • c is the polymer concentration determined from the DRI analysis
  • A2 is the second virial coefficient
  • ⁇ ( ⁇ ) is the form factor for a monodisperse random coil
  • K 0 is the optical constant for the system:
  • a high temperature Viscotek Corporation viscometer which has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers, is used to determine specific viscosity.
  • One transducer measures the total pressure drop across the detector, and the other, positioned between the two sides of the bridge, measures a differential pressure.
  • s for the solution flowing through the viscometer is calculated from their outputs.
  • the intrinsic viscosity, [ ⁇ ] at each point in the chromatogram, is calculated from the following equation:
  • n s c[n] + 0.3(c[n])2
  • the branching index (g' v i s ) is calculated using the output of the GPC-DRI-LS-VIS method as follows.
  • the average intrinsic viscosity, [Tl] a v > °f tne sample is calculated by:
  • the branching index g' v j s is defined as:
  • M v is the viscosity-average molecular weight based on molecular weights determined by LS analysis.
  • the polymer produced herein has a composition distribution breadth index (CDBI) of 50% or more, preferably 60% or more, preferably 70% or more, preferably 80% or more.
  • CDBI is a measure of the composition distribution of monomer within the polymer chains and is measured by the procedure described in WO 93/03093, published February 18, 1993, specifically columns 7 and 8, as well as in Wild et al, J. Poly. Sci., Poly. Phys. Ed., Vol. 20, p. 441, (1982) and US 5,008,204, including that fractions having a weight average molecular weight (Mw) below 15,000 are ignored when determining CDBI.
  • Mw weight average molecular weight
  • the polymer produced herein has two peaks in the TREF measurement.
  • Two peaks in the TREF measurement as used in this specification and the appended claims means the presence of two distinct normalized ELS (evaporation mass light scattering) response peaks in a graph of normalized ELS response (vertical or y axis) versus elution temperature (horizontal or x axis with temperature increasing from left to right) using the TREF method below.
  • a “peak” in this context means where the general slope of the graph changes from positive to negative with increasing temperature. Between the two peaks is a local minimum in which the general slope of the graph changes from negative to positive with increasing temperature.
  • the two distinct peaks are at least 3°C apart, more preferably at least 4°C apart, even more preferably at least 5°C apart. Additionally, both of the distinct peaks occur at a temperature on the graph above 20°C and below 120°C where the elution temperature is run to 0°C or lower. This limitation avoids confusion with the apparent peak on the graph at low temperature caused by material that remains soluble at the lowest elution temperature. Two peaks on such a graph indicates a bi-modal composition distribution (CD). Bimodal CD may also be determined by other methods known to those skilled in the art.
  • Temperature Rising Elution Fractionation (TREF) analysis is done using a CRYSTAF-TREF 200+ instrument from Polymer Char, S.A., Valencia, Spain.
  • the principles of TREF analysis and a general description of the particular apparatus to be used are given in the article Monrabal, B.; del Hierro, P. Anal. Bioanal. Chem., 2011 , 399, p. 1557.
  • Fig. 3 of the article is an appropriate schematic of the particular apparatus used; however, the connections to the 6-port valve shown in Fig.
  • a small volume (0.5 ml) of the solution is introduced into a column (15-cm long by 3/8" o.d.) packed with an inert support (of stainless steel balls) at 150°C, and the column temperature is stabilized at 140°C for 45 min.
  • the sample volume is then allowed to crystallize in the column by reducing the temperature to 30°C at a cooling rate of l °C/min.
  • the column is kept at 30°C for 15 min before injecting the ODCB flow (1 ml/min) into the column for 10 min to elute and measure the polymer that did not crystallize (soluble fraction).
  • the infrared detector used (Polymer Char IR4) generates an absorbance signal that is proportional to the concentration of polymer in the eluting flow.
  • a complete TREF curve is then generated by increasing the temperature of the column from 30 to 140°C at a rate of 2°C/min while maintaining the ODCB flow at 1 ml/min to elute and measure the dis
  • the polymer produced herein has a branching index (g'vis) of 0.95 or more, preferably 0.97 or more, preferably 0.98 or more.
  • the polymer produced herein has a bimodal composition distribution and a branching index (g'vis) of 0.95 or more, preferably 0.97 or more, preferably 0.98 or more.
  • the polymer produced herein has a bulk density of 0.25 g/cc or more, preferably 0.30 to 0.80 g/cc, preferably greater than 0.32 g/cc.
  • Bulk density is measured by quickly transferring (in 10 seconds) the sample powder into a graduated cylinder which overflows when exactly 100 cc is reached. No further powder is added at this point. The rate of powder addition prevents settling within the cylinder. The weight of the powder is divided by 100 cc to give the density.
  • the polymers produced herein comprise at least 0.1 wt% layered silicate where the layered silicate has an average aspect ratio (L/W) of 1.5 or more, preferably from 1.5 to 10, preferably from 2 to 5, preferably from 2 to 4, as determined by Transmission Electron Microscopy.
  • L/W average aspect ratio
  • the polymers produced herein comprise at least 0.1 wt% layered silicate where the layered silicate has an average aspect ratio (L/W) of 1.5 or more, preferably from 1.5 to 10, preferably from 2 to 5, preferably from 2 to 4, as determined by Transmission Electron Microscopy and have an Mw of 1,000,000 to 5,000,000 g/mol (preferably 1 ,500,000 to 4,000,000 g/mol) as measured by GPC.
  • L/W average aspect ratio
  • Average aspect ratio is determined by averaging the aspect ratio (length versus width) of multiple particles as shown in Transmission Electron Micrographs. Several TEM photographs of the sample are taken and 60 particles of layered silicate are identified and measured. For each of the 60 particles, the longest dimension is identified by drawing a line between the two points at the edge of the particle which are the furthest apart ("length"). Then the shortest dimension is identified by drawing a line between the two points at the edge of the particle which are the least distance apart ("width"). Length is then divided by width to obtain aspect ratio. The average aspect ratio is calculated as the arithmetical mean based on the aspect ratio of the 60 particles. Image-Pro PlusTM v 7.0.0 is used for image analysis.
  • Polyolefins prepared using the processes described herein find uses in all applications including fibers, injection molded parts, films, pipes, and wire and cable applications.
  • Examples include carpet fibers and primary and secondary carpet backing; slit tape applications, such as tarpaulins, erosion abatement screens, sand bags, fertilizer and feed bags, swimming pool covers, intermediate bulk container (IBC) bags; non-woven applications for spun-bonded, melt blown and thermobonded fibers; carded web applications, such as disposable diaper liners, feminine hygiene products, tarpaulins and tent fabrics, and hospital garments; apparel applications, such as socks, T-shirts, undergarments, bicycle shorts, sweat bands, football undershirts, hiking socks, and other outdoor sporting apparel; cordage applications, such as mooring and towing lines and rope; netting applications, such as safety fences and geogrids for soil stabilization; injection molded applications such as appliance parts in automatic dishwashers and clothes washers, hand tools, and kitchen appliances; consumer product applications, such as outdoor furniture,
  • polystyrene resins described herein may be used by themselves or blended with one or more additional polymers.
  • the polyolefin (preferably propylene or ethylene homopolymer or copolymer) produced herein is combined with one or more additional polymers prior to being formed into a film, molded part, or other article.
  • Useful additional polymers include polyethylene, isotactic polypropylene, highly isotactic polypropylene, syndiotactic polypropylene, random copolymer of propylene and ethylene, and/or butene, and/or hexene, polybutene, ethylene vinyl acetate, LDPE (low density polyethylene), LLDPE (linear low density polyethylene), HDPE (high density polyethylene), ethylene vinyl acetate, ethylene methyl acrylate, copolymers of acrylic acid, polymethylmethacrylate or any other polymers polymerizable by a high-pressure free radical process, polyvinylchloride, polybutene- 1 , isotactic polybutene, ABS resins, ethylene- propylene rubber (EPR), vulcanized EPR, EPDM (ethylene-propylene-diene monomer rubber), block copolymer, styrenic block copolymers, polyamides, polycarbonates, PET (polyethylene
  • This invention further relates to:
  • a process to polymerize olefins comprising:
  • a catalyst system comprising: 1) support comprising an organoaluminum treated layered silicate and inorganic oxide and 2) bisphenolate compound represented by the Formula (A):
  • M is a Group 4 transition metal
  • X 1 and X 2 are, independently, a univalent Ci to C2 0 hydrocarbyl radical, a Ci to C2 0 substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or X 1 and X 2 join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure;
  • each R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 , R 9 and R 10 is, independently, a hydrogen, a Ci to C 40 hydrocarbyl radical, a Ci to C 4 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or two or more of R 1 to R 10 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof;
  • Q is a neutral donor group
  • J is a C 7 to C 6 o fused polycyclic group, which optionally comprises up to 20 atoms from groups 15 and 16, where at least one ring is aromatic and where at least one ring, which may or may not be aromatic, has at least five members;
  • G is as defined for J or may be hydrogen, a Ci to C 6 o hydrocarbyl radical, a Ci to C 6 o substituted hydrocarbyl radical, a heteroatom or a heteroatom-containing group, or may independently form a C 4 to C 6 o cyclic or polycyclic ring structure with R 6 , R 7 , or R 8 , or a combination thereof; and
  • Y is a divalent Ci to C2 0 hydrocarbyl or divalent Ci to C2 0 substituted hydrocarbyl.
  • each R*, R", R 11 , R 12 , R 13 , R 14 , R 15 , R 16 , R 17 , R 18 , R 19 , R 20 , R 21 , R 22 , R 23 , R 24 , R 25 , R 26 , and R 27 is, independently, a hydrogen, a Ci to C 4 o hydrocarbyl radical, a Ci to C 4 o substituted hydrocarbyl radical a functional group comprising elements from groups 13 to 17 of the periodic table of the elements, or two or more of R 1 to R 28 may independently join together to form a C 4 to C 6 2 cyclic or polycyclic ring structure, or a combination thereof, or Rl and R* may independently join together to form a five- to eight-membered heterocycle;
  • Q* is a group 15 or 16 atom
  • z is 0 or 1 ;
  • J* is CR" or N
  • G* is CR" or N.
  • G and J or G* and J* are carbazolyl, substituted carbazolyl, indolyl, substituted indolyl, indolinyl, substituted indolinyl, imidazolyl, substituted imidazolyl, indenyl, substituted indenyl, indanyl, substituted indanyl, fluorenyl, or substituted fluorenyl.
  • Y is a divalent Ci to C 3 hydrocarbyl
  • Q 1 is NR' 2 , OR', SR', PR' 2
  • R' is as defined for R 1 in Embodiment 1
  • M is Zr, Hf or Ti and each X is, independently, as defined for X 1 in paragraph 1, preferably Q* is N, O, S, or P, and when Q* is N or P, z is 1 and when Q* is S or O, z is 0, and G* and J* are N or CR", where each R" is H or a Ci to Ci 2 alkyl.
  • the support is obtained by spray drying an aqueous slurry of trialkyl aluminum treated montmonllonite, where the alkyl is a CI to C12 alkyl group, and a sodium, potassium, lithium, or magnesium silicate, or a mixture thereof.
  • the support comprises at least 10 wt% montmorillonite, based upon the weight of the organoaluminum treated layered silicate and the inorganic oxide. 16. The process of any of paragraphs 1 to 15, wherein the support comprises 50 to 90 wt% montmorillonite, based upon the weight of the organoaluminum treated layered silicate and the inorganic oxide.
  • organoaluminum comprises trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n- octylaluminum, tri-iso-octylaluminum, triphenylaluminum, or a combination thereof.
  • An ethylene polymer having an Mw of 1 ,000,000 g/mol or more and comprising 0.1 to 5 wt% of a layered silicate derived from a supported catalyst used to produce the ethylene polymer, where the ethylene polymer has 1) no diffraction peak resulting from interlamellar spacing of the layered silicate present in the supported catalyst, and 2) a diffraction peak resulting from interlamellar spacing of the layered silicate of Z Angstroms or more, where Z 5X, where X is the diffraction peak resulting from interlamellar spacing of the layered silicate present in the supported catalyst, as measured by wide angle x-ray scattering.
  • NMR data of non-polymeric compounds was collected at room temperature in a 5 mm probe using either a Bruker or Varian NMR spectrometer operating with a If! frequency of 400 or 500 MHz. Data was recorded using a 30° flip angle RF pulse, 8 scans, with a delay of 5 seconds between pulses. Samples were prepared using approximately 5-10 mg of compound dissolved in approximately 1 mL of an appropriate deuterated solvent, as listed in the experimental examples.
  • NMR spectroscopic data of polymers was recorded in a 5 mm probe on a Varian NMR spectrometer at 120°C using a d 2 -l,l ,2,2-tetrachloroethane solution prepared from approximately 20 mg of polymer and 1 mL of solvent. Unless stated otherwise, data was recorded using a 30° flip angle RF pulse, 120 scans, with a delay of 5 seconds between pulses.
  • Catalyst A Catalyst B
  • the supernatant was decanted, and the crude product was purified over silica gel, eluting with a gradient of 0-20% ethyl acetate in hexane, to give the desired product (0.696g, 77%) as a white powder.
  • K10 montmorillonite was purchased from Sigma- Aldrich and used as received.
  • Montmorillonite KSF was purchased from Sigma-Aldrich.
  • Methylalumoxane 30 wt% in toluene was purchased from Albemarle and used as received.
  • Trimethyl aluminum, triethyl aluminum and tri-n-octyl aluminum were purchased from Akzo Nobel and used as received.
  • Support 1 was prepared by adding 2500 g of montmorillonite (K- 10, Sigma- Aldrich) to 3.4 1 of deionized water. A homogeneous slurry, with an agglomerate size dso typically in the range of 15 ⁇ , was achieved by stirring with a high-shear mixer for 60 min. Then 27 g of sodium silicate (reagent grade, Aldrich) were added to the mixture and homogenized for 5 min; achieving a final solids content of 30 wt%.
  • montmorillonite K- 10, Sigma- Aldrich
  • the obtained slurry was spray dried at a rate of 300 cc/min using a Bowen spray drier with an inlet temperature in the range of 716°F and 1100°F (380°C and 593°C), depending on feed flow, and a target outlet temperature of 320°F (160°C).
  • the product was recovered as a dry, flowing powder with an agglomerate size dso between 90 and 150 ⁇ , and moisture content between 17 and 6 wt%, depending on spray gas pressure.
  • the support was dried further at 121 °F (250°C) for 16 h and optionally calcined in air at 932°F (500°C) for 8 h.
  • Support 1 had a surface area (BET method)of 204 m 2 /g and a pore volume (BJH Adsorption cumulative volume) of 0.257cm 3 /g.
  • Montmorillonite KSF (Sigma Aldrich) was then treated according to the general procedure of Example 1 of US 7,220,695, i.e., Montmorillonite KSF (198.766g) was placed in a 2 L round bottom flask along with 1.40 L of 3 ⁇ 40 and 110 mL of concentrated sulfuric acid and stirred for 6hr at 90°C. The mixture was then allowed to stir overnight at room temperature. The mixture was filtered and the solid was was washed with 4xlL of H 2 0. The pH of the filtrate was monitored; when the pH was approximately 3 the washing was stopped and the solid was heated to 130°C while open to air.
  • Support 2 had a surface area (BET method)of 169 m 2 /g and a pore volume (BJH Adsorption cumulative volume) of 0.226cm 3 /g.
  • Support 1 (4.53 grams) was slurried in 30 milliters of toluene in a Celstir flask. Triethylaluminum (534. Omg, 4.598mmol) was added neat to the Celstir. The slurry stirred for 1 hour at 60°C. The solid was filtered, washed three times with 15 milliters of toluene and two times with pentane. The solid was dried under vacuum, giving 5.6 grams of gray solid as Support 4.
  • Support 4 had a surface area (BET method) of 169 m 2 /g and a pore volume (BJH Adsorption cumulative volume) of 0.226cm 3 /g.
  • Support 4 was slurried in 15 mL of toluene at high speed.
  • Catalyst A (29.6mg, 0.0284mmol) was dissolved in 10 mL of toluene and added to the slurry. The slurry stirred for 1 hour before being filtered, washed three times with 15 mL portions of toluene and twice with pentane. The solid was dried under vacuum, giving 0.7 grams of tan solid.
  • Support 4 was slurried in 15 mL of toluene at high speed.
  • Catalyst B 38.4mg, 0.0377mmol was dissolved in 5 mL of toluene and added to the slurry. The slurry stirred for 1 hour before being filtered, washed three times with 15 mL portions of toluene and twice with pentane. The solid was dried under vacuum, giving 0.9 grams of tan solid.
  • Solvents, polymerization grade toluene and isohexane were supplied by ExxonMobil Chemical Company and thoroughly dried and degassed prior to use. Polymerization grade ethylene was used and further purified by passing it through a series of columns: 500 cc Oxyclear cylinder from Labclear (Oakland, CA) followed by a 500 cc column packed with dried 3 A mole sieves purchased from Aldrich Chemical Company, and a 500 cc column packed with dried 5A mole sieves purchased from Aldrich Chemical Company. TnOAl (tri-n-octylaluminum, neat) was used as a 2 mmol/L solution in toluene.
  • Table A Ethylene Hexene Polymerization. Run condition: isohexane as solvent, 85°C, 130 psi ethylene pressure, 30 ⁇ of 1-hexene, 3.96 micromoles of triisobutylaluminum, 300 ppm hydrogen or 0 ppm hydrogen as noted in Table.
  • the GPC system was calibrated using polystyrene standards ranging from 580 - 3,390,000 g/mol. The system was operated at an eluent flow rate of 2.0 mL/minutes and an oven temperature of 165°C. 1 ,2,4-trichlorobenzene was used as the eluent. The polymer samples were dissolved in 1 ,2,4-trichlorobenzene at a concentration of 0.28 mg/mL. 250 uL of a polymer solution was injected into the system. The concentration of the polymer in the eluent was monitored using an IR detector. The molecular weights presented are relative to linear polystyrene standards and are uncorrected.
  • Samples for infrared analysis were prepared by depositing the stabilized polymer solution onto a silanized wafer (Part number SI 0860, Freeslate). By this method, approximately between 0.2 and 0.5 mg of polymer is deposited on the wafer cell. The samples were subsequently analyzed on a Brucker Vertex 70 FTIR spectrometer equipped with Pikes' MappIR specular reflectance sample accessory. Spectra, covering a spectral range of 5000 cm “1 to 350 cm “1 , were collected at a 0.5cm "1 resolution with 32 scans. For ethylene - 1-hexene copolymers, the wt% copolymer was determined via measurement of the methyl deformation band between 1382 to 1377cm "1 .
  • the peak height of this band was normalized by the combination and overtone band between 4300 to 4340cm "1 , which corrects for path length differences.
  • the normalized peak height was correlated to individual calibration curves from 1H NMR data to predict the wt% copolymer content within a concentration range of ⁇ 1.03 to 18.31 wt% for 1-hexene.
  • DSC Differential Scanning Calorimetry
  • compositions, an element or a group of elements are preceded with the transitional phrase “comprising,” it is understood that we also contemplate the same composition or group of elements with transitional phrases “consisting essentially of,” “consisting of,” “selected from the group of consisting of,” or “is” preceding the recitation of the composition, element, or elements and vice versa.

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Abstract

La présente invention concerne un procédé pour polymériser des oléfines consistant à : i) mettre en contact une ou plusieurs oléfines avec un système de catalyseur comprenant : 1) un support comprenant un silicate stratifié traité par un organoaluminium ainsi qu'un oxyde inorganique ; et 2) un composé bisphénolate ; et ii) obtenir un polymère oléfinique ayant un poids moléculaire élevé et dans lequel le silicate stratifié est dispersé. Le support se présente de préférence sous la forme de particules sphéroïdales.
PCT/US2016/047888 2015-10-02 2016-08-19 Procédé de polymérisation à l'aide de composés bisphénolate supportés sur des supports de silicate stratifié traité par un organoaluminium WO2017058391A1 (fr)

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Cited By (1)

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Publication number Priority date Publication date Assignee Title
US10927134B2 (en) 2018-08-28 2021-02-23 Exxonmobil Chemical Patents Inc. Bridged phenolate transition metal complexes, production, and uses thereof

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Publication number Priority date Publication date Assignee Title
US6399535B1 (en) * 1999-11-01 2002-06-04 W. R. Grace & Co.-Conn. Coordination catalyst systems employing agglomerated metal oxide/clay support-activator and method of their preparation
US7220695B2 (en) * 2004-01-07 2007-05-22 Exxonmobil Chemical Patents Inc. Supported activator
WO2013040276A1 (fr) * 2011-09-13 2013-03-21 California Institute Of Technology Complexes organométalliques à plusieurs métaux, et polymères, compositions, procédés et systèmes correspondants

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US6399535B1 (en) * 1999-11-01 2002-06-04 W. R. Grace & Co.-Conn. Coordination catalyst systems employing agglomerated metal oxide/clay support-activator and method of their preparation
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WO2013040276A1 (fr) * 2011-09-13 2013-03-21 California Institute Of Technology Complexes organométalliques à plusieurs métaux, et polymères, compositions, procédés et systèmes correspondants

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US10927134B2 (en) 2018-08-28 2021-02-23 Exxonmobil Chemical Patents Inc. Bridged phenolate transition metal complexes, production, and uses thereof

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