US20160347890A1 - Producing polyolefin products - Google Patents

Producing polyolefin products Download PDF

Info

Publication number
US20160347890A1
US20160347890A1 US15/117,363 US201515117363A US2016347890A1 US 20160347890 A1 US20160347890 A1 US 20160347890A1 US 201515117363 A US201515117363 A US 201515117363A US 2016347890 A1 US2016347890 A1 US 2016347890A1
Authority
US
United States
Prior art keywords
group
divalent
catalyst
substituted
canceled
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US15/117,363
Other languages
English (en)
Inventor
Sun-Chueh Kao
Francis C. Rix
Ching-Tai Lue
Mark G. Goode
Dongming Li
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Univation Technologies LLC
Original Assignee
Univation Technologies LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Univation Technologies LLC filed Critical Univation Technologies LLC
Priority to US15/117,363 priority Critical patent/US20160347890A1/en
Publication of US20160347890A1 publication Critical patent/US20160347890A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • 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
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J5/00—Manufacture of articles or shaped materials containing macromolecular substances
    • C08J5/18—Manufacture of films or sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B32—LAYERED PRODUCTS
    • B32B—LAYERED PRODUCTS, i.e. PRODUCTS BUILT-UP OF STRATA OF FLAT OR NON-FLAT, e.g. CELLULAR OR HONEYCOMB, FORM
    • B32B27/00—Layered products comprising a layer of synthetic resin
    • B32B27/32—Layered products comprising a layer of synthetic resin comprising polyolefins
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F17/00—Metallocenes
    • 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
    • C08F2/00—Processes of polymerisation
    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/34—Polymerisation in gaseous state
    • 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
    • C08F210/02—Ethene
    • 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
    • C08F210/18—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers with non-conjugated dienes, e.g. EPT 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
    • 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
    • C08F4/643—Component covered by group C08F4/64 with a metal or compound covered by group C08F4/44 other than an organo-aluminium compound
    • C08F4/6432—Component of C08F4/64 containing at least two different metals
    • 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
    • C08F4/65904—Component covered by group C08F4/64 containing a transition metal-carbon bond in combination with another component of C08F4/64
    • 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
    • C08F4/72—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from metals not provided for in group C08F4/44
    • C08F4/74—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from metals not provided for in group C08F4/44 selected from refractory metals
    • C08F4/76—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from metals not provided for in group C08F4/44 selected from refractory metals selected from titanium, zirconium, hafnium, vanadium, niobium or tantalum
    • 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
    • C08F210/04—Monomers containing three or four carbon atoms
    • C08F210/08—Butenes
    • 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
    • C08F210/14—Monomers containing five or more carbon atoms
    • 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
    • C08F2410/01—Additive used together with the catalyst, excluding compounds containing Al or B
    • 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
    • C08F2410/02—Anti-static agent incorporated into the catalyst
    • 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
    • C08F2420/00—Metallocene catalysts
    • 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
    • C08F2420/00—Metallocene catalysts
    • C08F2420/01—Cp or analog bridged to a non-Cp X neutral donor
    • 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
    • C08F2420/00—Metallocene catalysts
    • C08F2420/08—Heteroatom bridge, i.e. Cp or analog where the bridging atom linking the two Cps or analogs is a heteroatom different from Si
    • 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
    • C08F2420/00—Metallocene catalysts
    • C08F2420/12—Long bridge, i.e. Cp or analog where the bridging unit linking the two Cps or analogs is composed of at least two atoms which are not part of a cycle and which are not an ethylene bridge
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/01—High molecular weight, e.g. >800,000 Da.
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/02—Low molecular weight, e.g. <100,000 Da.
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/03—Narrow molecular weight distribution, i.e. Mw/Mn < 3
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/08—Low density, i.e. < 0.91 g/cm3
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/09—Long chain branches
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/10—Short chain branches
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/11—Melt tension or melt strength
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/12—Melt flow index or melt flow ratio
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/13—Environmental stress cracking resistance
    • 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
    • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
    • C08F2500/18—Bulk density
    • 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
    • C08F2800/00—Copolymer characterised by the proportions of the comonomers expressed
    • C08F2800/20—Copolymer characterised by the proportions of the comonomers expressed as weight or mass percentages
    • 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
    • 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
    • C08F4/6592—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
    • C08F4/65922—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring containing at least two cyclopentadienyl rings, fused or not
    • C08F4/65925—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring containing at least two cyclopentadienyl rings, fused or not two cyclopentadienyl rings being mutually non-bridged
    • 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
    • C08F4/6592—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
    • C08F4/65922—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring containing at least two cyclopentadienyl rings, fused or not
    • C08F4/65927—Component covered by group C08F4/64 containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring containing at least two cyclopentadienyl rings, fused or not two cyclopentadienyl rings being mutually bridged
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C08J2323/04—Homopolymers or copolymers of ethene
    • C08J2323/08—Copolymers of ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
    • C08L23/02—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers not modified by chemical after-treatment
    • C08L23/04—Homopolymers or copolymers of ethene
    • C08L23/08—Copolymers of ethene
    • C08L23/0807—Copolymers of ethene with unsaturated hydrocarbons only containing more than three carbon atoms
    • C08L23/0815—Copolymers of ethene with aliphatic 1-olefins
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • Ethylene alpha-olefin (polyethylene) copolymers are typically produced in a low pressure reactor, utilizing, for example, solution, slurry, or gas phase polymerization processes. Polymerization takes place in the presence of catalyst systems such as those employing, for example, a Ziegler-Natta catalyst, a chromium based catalyst, a metallocene catalyst, or combinations thereof.
  • catalyst systems such as those employing, for example, a Ziegler-Natta catalyst, a chromium based catalyst, a metallocene catalyst, or combinations thereof.
  • a number of catalyst compositions containing single site, e.g., metallocene, catalysts have been used to prepare polyethylene copolymers, producing relatively homogeneous copolymers at good polymerization rates.
  • single site catalyst compositions such as metallocene catalysts
  • Single site catalysts are catalytic compounds in which each catalyst molecule contains one or only a few polymerization sites.
  • Single site catalysts often produce polyethylene copolymers that have a narrow molecular weight distribution. Although there are single site catalysts that can produce broader molecular weight distributions, these catalysts often show a narrowing of the molecular weight distribution as the reaction temperature is increased, for example, to increase production rates.
  • a single site catalyst will often incorporate comonomer among the molecules of the polyethylene copolymer at a relatively uniform rate. The molecular weight distribution and the amount of comonomer incorporation can be used to determine a composition distribution.
  • composition distribution of an ethylene alpha-olefin copolymer refers to the distribution of comonomer, which form short chain branches, among the molecules that comprise the polyethylene polymer.
  • the resin is said to have a “broad” composition distribution.
  • the amount of comonomer per 1000 carbons is similar among the polyethylene molecules of different chain lengths, the composition distribution is said to be “narrow”.
  • composition distribution is known to influence the properties of copolymers, for example, stiffness, toughness, extractable content, environmental stress crack resistance, and heat sealing, among other properties.
  • the composition distribution of a polyolefin may be readily measured by methods known in the art, for example, Temperature Raising Elution Fractionation (TREF) or Crystallization Analysis Fractionation (CRYSTAF).
  • Resins having a broad orthogonal composition distribution in which the comonomer is incorporated predominantly in the high molecular weight chains can lead to improved physical properties, for example toughness properties and environmental stress crack resistance (ESCR). Because of the improved physical properties of resins with orthogonal composition distributions needed for commercially desirable products, there exists a need for controlled techniques for forming polyethylene copolymers having a broad orthogonal composition distribution.
  • BOCD broad orthogonal composition distribution
  • ESCR environmental stress crack resistance
  • An exemplary embodiment described herein provides a method of polymerizing olefins to produce a polyolefin polymer with a multimodal composition distribution, including contacting ethylene and a comonomer with a catalyst system.
  • the catalyst system includes a first catalyst compound and a second catalyst compound that are co-supported to form a commonly supported catalyst system.
  • the first catalyst compound includes a compound with the following formula:
  • each R 1 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group.
  • At least one R 1 and at least one R 2 is a hydrocarbyl or substituted hydrocarbyl group.
  • Adjacent groups R 1 and R 2 groups may be coupled to form a ring.
  • Each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group, or a divalent radical that links to an R 1 or R 2 group.
  • the second catalyst compound comprises the following formula:
  • each R 3 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group, wherein each R 3 may be the same or different.
  • Each X is independently a leaving group selected from a labile hydrocarbyl, a substituted hydrocarbyl, a heteroatom group, or a divalent radical that links to an R 3 group.
  • Another embodiment provides a catalyst composition including a first catalyst compound and a second catalyst compound that are co-supported forming a commonly supported catalyst system.
  • the first catalyst compound includes a compound with the following formula:
  • each R 1 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group.
  • At least one R 1 and at least one R 2 is a hydrocarbyl or substituted hydrocarbyl group.
  • Adjacent groups R 1 and R 2 groups may be coupled to form a ring.
  • Each X is independently a leaving group selected from a labile hydrocarbyl, substituted hydrocarbyl, or heteroatom group, or a divalent radical that links to an R 1 or R 2 group.
  • the second catalyst compound comprises the following formula:
  • each R 3 is independently H, a hydrocarbyl group, a substituted hydrocarbyl group, or a heteroatom group, wherein each R 3 may be the same or different.
  • Each X is independently a leaving group selected from a labile hydrocarbyl, a substituted hydrocarbyl, a heteroatom group, or a divalent radical that links to an R 3 group.
  • FIG. 1 is a schematic of a gas-phase reactor system, showing the addition of at least two catalysts, at least one of which is added as a trim catalyst.
  • FIG. 2 is a plot of a series of polymers that were prepared to test the relative abilities of a series of metallocene catalysts to prepare a resin having about a 1 melt index (MI) and a density (D) of about 0.92.
  • MI melt index
  • D density
  • FIG. 3 is a plot of the series of polymers of FIG. 2 , showing the melt index ratio (MIR) of the series of polymers made by different metallocene (MCN) catalysts.
  • MIR melt index ratio
  • FIG. 4 is a flow chart of a method for making a co-supported polymerization catalyst.
  • a pre-catalyst is a catalyst compound prior to exposure to activator.
  • LLDPE linear low-density polyethylene film
  • an ethylene hexene copolymer with a molecular weight of between about 90 Kg/mol and 110 Kg/mol, or about 100 Kg/mol and an average density of between about 0.9 and 0.925, or about 0.918.
  • the typical MWD for linear metallocene resins is 2.5-3.5.
  • Blend studies indicate that it would be desirable to broaden this distribution by employing two catalysts that each provides different average molecular weights.
  • the ratio of the Mw for the low molecular weight component and the high molecular weight component would be between 1:1 and 1:10, or about 1:2 and 1:5.
  • the density of a polyethylene copolymer provides an indication of the incorporation of comonomer into a polymer, with lower densities indicating higher incorporation.
  • the difference in the densities of the low molecular weight (LMW) component and the high molecular weight (HMW) component would preferably be greater than about 0.02, or greater than about 0.04 with the HMW component having a lower density than the LMW component.
  • LMW low molecular weight
  • HMW high molecular weight
  • the difference in density requires around around around a 1.5:1 or preferably about 2:1, or more preferably about 3:1 or more preferably a 4:1 or even a greater than 4:1 difference difference in comonomer incorporation ability.
  • LCB long chain branching
  • MWD and SCBD can be adjusted by changing the relative amount of the two pre-catalysts on the support. This may be adjusted during the formation of the pre-catalysts, for example, by supporting two catalysts on a single support.
  • the relative amounts of the pre-catalysts can be adjusted by adding one of the components to a catalyst mixture en-route to the reactor in a process termed “trim.” Feedback of polymer property data can be used to control the amount of catalyst addition.
  • MNs Metallocenes
  • a variety of resins with different MWD, SCBD, and LCBD may be prepared from a limited number of catalysts.
  • the pre-catalysts should trim well onto activator supports. Two parameters that benefit this are solubility in alkane solvents and rapid supportation on the catalyst slurry en-route to the reactor. This favors the use of MCNs to achieve controlled MWD, SCBD, and LCBD. Techniques for selecting catalysts that can be used to generate targeted molecular weight compositions, including BOCD polymer systems, are disclosed herein.
  • the first section discusses catalyst compounds that can be used in embodiments.
  • the second section discusses generating catalyst slurrys that may be used for implementing the techniques described.
  • the third section discusses catalyst supports that may be used.
  • the fourth section discusses catalyst activators that may be used.
  • the fifth section discusses the catalyst component solutions that may be used to add additional catalysts in trim systems.
  • Gas phase polymerizations may use static control or continuity agents, which are discussed in the sixth section.
  • a gas-phase polymerization reactor with a trim feed system is discussed in the seventh section.
  • the use of the catalyst composition to control product properties is discussed in an eighth section and an exemplary polymerization process is discussed in a ninth section. Examples of the implementation of the procedures discussed is incorporated into a tenth section.
  • Metallocene catalyst compounds can include “half sandwich” and/or “full sandwich” compounds having one or more Cp ligands (cyclopentadienyl and ligands isolobal to cyclopentadienyl) bound to at least one Group 3 to Group 12 metal atom, and one or more leaving group(s) bound to the at least one metal atom.
  • the Cp ligands are one or more rings or ring system(s), at least a portion of which includes ⁇ -bonded systems, such as cycloalkadienyl ligands and heterocyclic analogues.
  • the ring(s) or ring system(s) typically include atoms selected from the group consisting of Groups 13 to 16 atoms, and, in a particular exemplary embodiment, the atoms that make up the Cp ligands are selected from the group consisting of carbon, nitrogen, oxygen, silicon, sulfur, phosphorous, germanium, boron, aluminum, and combinations thereof, where carbon makes up at least 50% of the ring members.
  • the Cp ligand(s) are selected from the group consisting of substituted and unsubstituted cyclopentadienyl ligands and ligands isolobal to cyclopentadienyl, non-limiting examples of which include cyclopentadienyl, indenyl, fluorenyl and other structures.
  • Such ligands include cyclopentadienyl, cyclopentaphenanthreneyl, indenyl, benzindenyl, fluorenyl, octahydrofluorenyl, cyclooctatetraenyl, cyclopentacyclododecene, phenanthrindenyl, 3,4-benzofluorenyl, 9-phenylfluorenyl, 8-H-cyclopent[a]acenaphthylenyl, 7-H-dibenzofluorenyl, indeno[1,2-9]anthrene, thiophenoindenyl, thiophenofluorenyl, hydrogenated versions thereof (e.g., 4,5,6,7-tetrahydroindenyl, or “H 4 Ind”), substituted versions thereof (as discussed and described in more detail below), and heterocyclic versions thereof.
  • H 4 Ind hydrogenated versions thereof
  • the metal atom “M” of the metallocene catalyst compound can be selected from the group consisting of Groups 3 through 12 atoms and lanthanide Group atoms in one exemplary embodiment; and selected from the group consisting of Groups 3 through 10 atoms in a more particular exemplary embodiment, and selected from the group consisting of Sc, Ti, Zr, Hf, V, Nb, Ta, Mn, Re, Fe, Ru, Os, Co, Rh, Ir, and Ni in yet a more particular exemplary embodiment; and selected from the group consisting of Groups 4, 5, and 6 atoms in yet a more particular exemplary embodiment, and Ti, Zr, Hf atoms in yet a more particular exemplary embodiment, and Hf in yet a more particular exemplary embodiment.
  • the oxidation state of the metal atom “M” can range from 0 to +7 in one exemplary embodiment; and in a more particular exemplary embodiment, can be +1, +2, +3, +4, or +5; and in yet a more particular exemplary embodiment can be +2, +3 or +4.
  • the groups bound to the metal atom “M” are such that the compounds described below in the formulas and structures are electrically neutral, unless otherwise indicated.
  • the Cp ligand forms at least one chemical bond with the metal atom M to form the “metallocene catalyst compound.”
  • the Cp ligands are distinct from the leaving groups bound to the catalyst compound in that they are not highly susceptible to substitution/abstraction reactions.
  • the one or more metallocene catalyst compounds can be represented by the formula (I):
  • the ligands represented by Cp A and Cp B in formula (I) can be the same or different cyclopentadienyl ligands or ligands isolobal to cyclopentadienyl, either or both of which can contain heteroatoms and either or both of which can be substituted by a group R.
  • Cp A and Cp B are independently selected from the group consisting of cyclopentadienyl, indenyl, tetrahydroindenyl, fluorenyl, and substituted derivatives of each.
  • each Cp A and Cp B of formula (I) can be unsubstituted or substituted with any one or combination of substituent groups R.
  • substituent groups R as used in structure (I) as well as ring substituents in structures Va-d, discussed and described below, include groups selected from the group consisting of hydrogen radicals, alkyls, alkenyls, alkynyls, cycloalkyls, aryls, acyls, aroyls, alkoxys, aryloxys, alkylthiols, dialkylamines, alkylamidos, alkoxycarbonyls, aryloxycarbonyls, carbomoyls, alkyl- and dialkyl-carbamoyls, acyloxys, acylaminos, aroylaminos, and combinations thereof More particular non-limiting examples of alkyl substituents R associated with formulas (I) through (Va-d) include methyl,
  • hydrocarbyl substituents, or groups are made up of between 1 and 100 or more carbon atoms, the remainder being hydrogen.
  • hydrocarbyl substituents include linear or branched or cyclic: alkyl radicals; alkenyl radicals; alkynyl radicals; cycloalkyl radicals; aryl radicals; alkylene radicals, or a combination thereof
  • Non-limiting examples include methyl, ethyl, propyl, butyl, pentyl, hexyl, cyclopentyl, cyclohexyl; olefinically unsaturated substituents including vinyl-terminated ligands (for example but-3-enyl, prop-2-enyl, hex-5-enyl and the like), benzyl or phenyl groups and the like, including all their isomers, for example tertiary butyl, isopropyl, and the like.
  • substituted hydrocarbyl substituents, or groups are made up of between 1 and 100 or more carbon atoms, the remainder being hydrogen, fluorine, chlorine, bromine, iodine, oxygen, sulfur, nitrogen, phosphorous, boron, silicon, germanium or tin atoms or other atom systems tolerant of olefin polymerization systems.
  • Substituted hydrocarbyl substituents are carbon based radicals.
  • Non-limiting examples of substituted hydrocarbyl substituents trifluoromethyl radical, trimethylsilanemethyl (Me3SiCH 2-) radicals.
  • heteroatom substituents are fluorine, chlorine, bromine, iodine, oxygen, sulfur, nitrogen, phosphorous, boron, silicon, germanium or tin based radicals. They may be the heteroatom atom by itself Further, heteroatom substituents include organometalloid radicals.
  • heteroatom substituents include chloro radicals, fluoro radicals, methoxy radicals, diphenyl amino radicals, thioalkyls, thioalkenyls, trimethylsilyl radicals, dimethyl aluminum radicals, alkoxydihydrocarbylsilyl radicals, siloxydiydrocabylsilyl radicals, tris(perflourophenyl)boron and the like.
  • radicals include substituted alkyls and aryls such as, for example, fluoromethyl, fluroethyl, difluroethyl, iodopropyl, bromohexyl, chlorobenzyl, hydrocarbyl substituted organometalloid radicals including trimethylsilyl, trimethylgermyl, methyldiethylsilyl, and the like, and halocarbyl-substituted organometalloid radicals, including tris(trifluoromethyl)silyl, methylbis(difluoromethyl)silyl, bromomethyldimethylgermyl and the like; and disubstituted boron radicals including dimethylboron, for example; and disubstituted Group 15 radicals including dimethylamine, dimethylphosphine, diphenylamine, methylphenylphosphine, as well as Group 16 radicals including methoxy, ethoxy, propoxy, phenoxy, methyl
  • substituent groups R include, but are not limited to, olefins such as olefinically unsaturated substituents including vinyl-terminated ligands such as, for example, 3-butenyl, 2-propenyl, 5-hexenyl, and the like.
  • olefins such as olefinically unsaturated substituents including vinyl-terminated ligands such as, for example, 3-butenyl, 2-propenyl, 5-hexenyl, and the like.
  • at least two R groups are joined to form a ring structure having from 3 to 30 atoms selected from the group consisting of carbon, nitrogen, oxygen, phosphorous, silicon, germanium, aluminum, boron, and combinations thereof.
  • a substituent group R such as 1-butanyl can form a bonding association to the element M.
  • Each X in the formula (I) above and for the formula/structures (II) through (Va-d) below is independently selected from the group consisting of: any leaving group, in one exemplary embodiment; halogen ions, hydrides, C 1 to C 12 alkyls, C 2 to C 12 alkenyls, C 6 to C 12 aryls, C 7 to C 20 alkylaryls, C 1 to C 12 alkoxys, C 6 to C 16 aryloxys, C 7 to C 8 alkylaryloxys, C 1 to C 12 fluoroalkyls, C 6 to C 12 fluoroaryls, and C 1 to C 12 heteroatom-containing hydrocarbons and substituted derivatives thereof, in a more particular exemplary embodiment; hydride, halogen ions, C 1 to C 6 alkyls, C 2 to C 6 alkenyls, C 7 to C 18 alkylaryls, C 1 to C 6 alkoxys, C 6 to C 14 aryloxys, C 7 to
  • X groups include amines, phosphines, ethers, carboxylates, dienes, hydrocarbon radicals having from 1 to 20 carbon atoms, fluorinated hydrocarbon radicals (e.g., —C 6 F 5 (pentafluorophenyl)), fluorinated alkylcarboxylates (e.g., CF 3 C(O)O ⁇ ), hydrides, halogen ions and combinations thereof
  • X ligands include alkyl groups such as cyclobutyl, cyclohexyl, methyl, heptyl, tolyl, trifluoromethyl, tetramethylene, pentamethylene, methylidene, methyoxy, ethyoxy, propoxy, phenoxy, bis(N-methylanilide), dimethylamide, dimethylphosphide radicals and the like.
  • two or more X's form a part of a fused ring or ring system.
  • X can be a leaving group selected from the group consisting of chloride ions, bromide ions, C 1 to C io alkyls, and C 2 to C 12 alkenyls, carboxylates, acetylacetonates, and alkoxides.
  • the metallocene catalyst compound includes those of formula (I) where Cp A and Cp B are bridged to each other by at least one bridging group, (A), such that the structure is represented by formula (II):
  • bridged metallocenes These bridged compounds represented by formula (II) are known as “bridged metallocenes.”
  • the elements Cp A , Cp B , M, X and n in structure (II) are as defined above for formula (I); where each Cp ligand is chemically bonded to M, and (A) is chemically bonded to each Cp.
  • the bridging group (A) can include divalent hydrocarbon groups containing at least one Group 13 to 16 atom, such as, but not limited to, at least one of a carbon, oxygen, nitrogen, silicon, aluminum, boron, germanium, tin atom, and combinations thereof; where the heteroatom can also be C 1 to C 12 alkyl or aryl substituted to satisfy neutral valency.
  • the bridging group (A) can also include substituent groups R as defined above (for formula (I)) including halogen radicals and iron.
  • the bridged metallocene catalyst compound of formula (II) includes two or more bridging groups (A).
  • (A) can be a divalent bridging group bound to both Cp A and Cp B selected from the group consisting of divalent C 1 to C 20 hydrocarbyls and C 1 to C 20 heteroatom containing hydrocarbonyls, where the heteroatom containing hydrocarbonyls include from one to three heteroatoms.
  • the bridging group (A) can include methylene, ethylene, ethylidene, propylidene, isopropylidene, diphenylmethylene, 1,2-dimethylethylene, 1,2-diphenylethylene, 1,1,2,2-tetramethylethylene, dimethylsilyl, diethylsilyl, methyl-ethylsilyl, trifluoromethylbutylsilyl, bis(trifluoromethyl)silyl, di(n-butyl)silyl, di(n-propyl)silyl, di(i-propyl)silyl, di(n-hexyl)silyl, dicyclohexylsilyl, diphenylsilyl, cyclohexylphenylsilyl, t-butylcyclohexylsilyl, di(t-butylphenyl)silyl, di(p-tolyl)silyl, and the corresponding moieties where the
  • the bridging group (A) can also include —Si(hydrocarbyl)2-O-(hydrocarbyl)2Si-Si(substitutedhydrocarbyl)2-O-(substitutedhydrocarbyl)2Si— groups and the like such as —SiMe2-O—SiMe2- and —SiPh2-O—SiPh2-.
  • the bridging group (A) can also be cyclic, having, for example, 4 to 10 ring members; in a more particular exemplary embodiment, bridging group (A) can have 5 to 7 ring members.
  • the ring members can be selected from the elements mentioned above, and, in a particular embodiment, can be selected from one or more of B, C, Si, Ge, N, and O.
  • Non-limiting examples of ring structures which can be present as, or as part of, the bridging moiety are cyclobutylidene, cyclopentylidene, cyclohexylidene, cycloheptylidene, cyclooctylidene and the corresponding rings where one or two carbon atoms are replaced by at least one of Si, Ge, N and O. In one or more embodiments, one or two carbon atoms can be replaced by at least one of Si and Ge.
  • the bonding arrangement between the ring and the Cp groups can be cis-, trans-, or a combination thereof.
  • the cyclic bridging groups (A) can be saturated or unsaturated and/or can carry one or more substituents and/or can be fused to one or more other ring structures. If present, the one or more substituents can be, in at least one specific embodiment, selected from the group consisting of hydrocarbyl (e.g., alkyl, such as methyl) and halogen (e.g., F, Cl).
  • hydrocarbyl e.g., alkyl, such as methyl
  • halogen e.g., F, Cl
  • the one or more Cp groups to which the above cyclic bridging moieties can optionally be fused can be saturated or unsaturated, and are selected from the group consisting of those having 4 to 10, more particularly 5, 6, or 7 ring members (selected from the group consisting of C, N, O, and S in a particular exemplary embodiment) such as, for example, cyclopentyl, cyclohexyl and phenyl.
  • these ring structures can themselves be fused such as, for example, in the case of a naphthyl group.
  • these (optionally fused) ring structures can carry one or more substituents.
  • substituents are hydrocarbyl (particularly alkyl) groups and halogen atoms.
  • the ligands Cp A and Cp B of formula (I) and (II) can be different from each other.
  • the ligands Cp A and Cp B of formula (I) and (II) can be the same.
  • the metallocene catalyst compound can include bridged mono-ligand metallocene compounds (e.g., mono cyclopentadienyl catalyst components).
  • metallocene catalyst components discussed and described above include their structural or optical or enantiomeric isomers (racemic mixture), and, in one exemplary embodiment, can be a pure enantiomer.
  • a single, bridged, asymmetrically substituted metallocene catalyst compound having a racemic and/or meso isomer does not, itself, constitute at least two different bridged, metallocene catalyst components.
  • the amount of the transition metal component of the one or more metallocene catalyst compounds in the catalyst system can range from a low of about 0.0.01 wt. %, about 0.2 wt %, about 3 wt. %, about 0.5 wt. %, or about 0.7 wt. % to a high of about 1 wt. %, about 2 wt. %, about 2.5 wt. %, about 3 wt. %, about 3.5 wt. %, or about 4 wt. %, based on the total weight of the catalyst system.
  • the “metallocene catalyst compound” can include any combination of any “embodiment” discussed and described herein.
  • the metallocene catalyst compound can include, but is not limited to, bis(n-propylcyclopentadienyl) hafnium (CH 3 ) 2 , bis(n-propylcyclopentadienyl) hafnium F 2 , bis(n-propylcyclopentadienyl) hafnium Cl 2 , or bis(n-butyl, methyl cyclopentadienyl) zirconium Cl 2 , or any combination thereof
  • sCGC supported constrained geometry catalysts
  • the sCGC catalyst may include a borate ion.
  • the borate anion is represented by the formula [BQ 4-z′ (G q (T-H) r ) z′ ] d- , wherein: B is boron in a valence state of 3; Q is selected from the group consisting of hydride, dihydrocarbylamido, halide, hydrocarbyloxide, hydrocarbyl, and substituted-hydrocarbyl radicals; z′ is an integer in a range from 1 to 4; G is a polyvalent hydrocarbon radical having r+1 valencies bonded to M′ and r groups (T-H); q is an integer, 0 or 1; the group (T-H) is a radical wherein T includes O, S, NR, or PR, the O, S, N or P atom of which is bonded to hydrogen atom H, wherein R is a hydrocarbyl radical, a trihydrocarbylsilyl radical, a trihydrocarbyl germyl radical or hydrogen; r is an integer
  • the borate ion may be representative by the formula [BQ 4-z′ (G q (T-M o R C x-1 X a y ) r ) z′ ] d ⁇ , wherein: B is boron in a valence state of 3; Q is selected from the group consisting of hydride, dihydrocarbylamido, halide, hydrocarbyloxide, hydrocarbyl, and substituted-hydrocarbyl radicals; z′ is an integer in a range from 1 to 4; G is a polyvalent hydrocarbon radical having r+1 valencies bonded to B and r groups (T-M o R C x-1 X a y ); q is an integer, 0 or 1; the group (T-M o R C x-1 X a y ) is a radical wherein T includes O, S, NR, or PR, the O, S, N or P atom of which is bonded to M o , wherein
  • the catalyst system can include other single site catalysts such as Group 15-containing catalysts.
  • the catalyst system can include one or more second catalysts in addition to the single site catalyst compound such as chromium-based catalysts, Ziegler-Natta catalysts, one or more additional single-site catalysts such as metallocenes or Group 15-containing catalysts, bimetallic catalysts, and mixed catalysts.
  • the catalyst system can also include AlCl 3 , cobalt, iron, palladium, or any combination thereof.
  • Examples of structures of MCN compounds that may be used in embodiments include the hafnium compound shown as formula (II), the zirconium compounds shown as formulas (IV-A-C), and bridged zirconium compounds, shown as formulas (V-A-B).
  • each of these substituents may independently be a methyl group (Me), a chloro group (Cl), a fluoro group (F), or any number of other groups, including organic groups, or heteroatom groups. Further, these substituents will change during the reaction, as a pre-catalyst is converted to the active catalyst for the reaction. Further, any number of other substituents may be used on the ring structures, including any of the substituents described above with respect to formulas (I) and (II).
  • the catalyst system can include one or more Group 15 metal-containing catalyst compounds, such as [(2,3,4,5,6 Me 5 C 6 N)CH 2 CH 2 ] 2 NHZrBn 2 , where Bn is a benzyl group.
  • the Group 15 metal-containing compound generally includes a Group 3 to 14 metal atom, a Group 3 to 7, or a Group 4 to 6 metal atom.
  • the Group 15 metal-containing compound includes a Group 4 metal atom bound to at least one leaving group and also bound to at least two Group 15 atoms, at least one of which is also bound to a Group 15 or 16 atom through another group.
  • At least one of the Group 15 atoms is also bound to a Group 15 or 16 atom through another group which may be a C 1 to C 20 hydrocarbon group, a heteroatom containing group, silicon, germanium, tin, lead, or phosphorus, wherein the Group 15 or 16 atom may also be bound to nothing or a hydrogen, a Group 14 atom containing group, a halogen, or a heteroatom containing group, and wherein each of the two Group 15 atoms are also bound to a cyclic group and can optionally be bound to hydrogen, a halogen, a heteroatom or a hydrocarbyl group, or a heteroatom containing group.
  • the Group 15-containing metal compounds can be described more particularly with formulas (VI) or (VII):
  • M is a Group 3 to 12 transition metal or a Group 13 or 14 main group metal, a Group 4, 5, or 6 metal.
  • M is a Group 4 metal, such as zirconium, titanium or hafnium.
  • Each X is independently a leaving group, such as an anionic leaving group.
  • the leaving group may include a hydrogen, a hydrocarbyl group, a heteroatom, a halogen, or an alkyl; y is 0 or 1 (when y is 0 group L′ is absent).
  • the term ‘n’ is the oxidation state of M. In various embodiments, n is +3, +4, or +5. In many embodiments, n is +4.
  • m represents the formal charge of the YZL or the YZL′ ligand, and is 0, ⁇ 1, ⁇ 2 or ⁇ 3 in various embodiments. In many embodiments, m is ⁇ 2.
  • L is a Group 15 or 16 element, such as nitrogen; L′ is a Group 15 or 16 element or Group 14 containing group, such as carbon, silicon or germanium.
  • Y is a Group 15 element, such as nitrogen or phosphorus. In many embodiments, Y is nitrogen.
  • Z is a Group 15 element, such as nitrogen or phosphorus. In many embodiments, Z is nitrogen.
  • R 1 and R 2 are, independently, a C 1 to C 20 hydrocarbon group, a heteroatom containing group having up to twenty carbon atoms, silicon, germanium, tin, lead, or phosphorus.
  • R 1 and R 2 are a C 2 to C 20 alkyl, aryl, or aralkyl group, such as a linear, branched, or cyclic C 2 to C 20 alkyl group, or a C 2 to C 6 hydrocarbon group.
  • R 1 and R 2 may also be interconnected to each other.
  • R 3 may be absent or may be a hydrocarbon group, a hydrogen, a halogen, a heteroatom containing group.
  • R 3 is absent or a hydrogen, or a linear, cyclic or branched alkyl group having 1 to 20 carbon atoms.
  • R 4 and R 5 are independently an alkyl group, an aryl group, substituted aryl group, a cyclic alkyl group, a substituted cyclic alkyl group, a cyclic aralkyl group, a substituted cyclic aralkyl group or multiple ring system, often having up to 20 carbon atoms.
  • R 4 and R 5 have between 3 and 10 carbon atoms, or are a C 1 to C 20 hydrocarbon group, a C 1 to C 20 aryl group or a C 1 to C 20 aralkyl group, or a heteroatom containing group.
  • R 4 and R 5 may be interconnected to each other.
  • R 6 and R 7 are independently absent, hydrogen, an alkyl group, halogen, heteroatom, or a hydrocarbyl group, such as a linear, cyclic, or branched alkyl group having 1 to 20 carbon atoms.
  • R 6 and R 7 are absent.
  • R* may be absent, or may be a hydrogen, a Group 14 atom containing group, a halogen, or a heteroatom containing group.
  • R 1 and R 2 may also be interconnected” it is meant that R 1 and R 2 may be directly bound to each other or may be bound to each other through other groups.
  • R 4 and R 5 may also be interconnected” it is meant that R 4 and R 5 may be directly bound to each other or may be bound to each other through other groups.
  • An alkyl group may be linear, branched alkyl radicals, alkenyl radicals, alkynyl radicals, cycloalkyl radicals, aryl radicals, acyl radicals, aroyl radicals, alkoxy radicals, aryloxy radicals, alkylthio radicals, dialkylamino radicals, alkoxycarbonyl radicals, aryloxycarbonyl radicals, carbomoyl radicals, alkyl- or dialkyl-carbamoyl radicals, acyloxy radicals, acylamino radicals, aroylamino radicals, straight, branched or cyclic, alkylene radicals, or combination thereof.
  • An aralkyl group is defined to be a substituted aryl group.
  • R 4 and R 5 are independently a group represented by the following formula (VIII).
  • R 8 to R 12 are each independently hydrogen, a C 1 to C 40 alkyl group, a halide, a heteroatom, a heteroatom containing group containing up to 40 carbon atoms.
  • R 8 to R 12 are a C 1 to C 20 linear or branched alkyl group, such as a methyl, ethyl, propyl, or butyl group. Any two of the R groups may form a cyclic group and/or a heterocyclic group.
  • the cyclic groups may be aromatic.
  • R 9 , R 10 and R 12 are independently a methyl, ethyl, propyl, or butyl group (including all isomers).
  • R 9 , R 16 and R 12 are methyl groups, and R 8 and R 11 are hydrogen.
  • R 4 and R 5 are both a group represented by the following formula (IX).
  • M is a Group 4 metal, such as zirconium, titanium, or hafnium. In many embodiments, M is zirconium.
  • Each of L, Y, and Z may be a nitrogen.
  • Each of R 1 and R 2 may be —CH 2 —CH 2 —.
  • R 3 may be hydrogen, and R 6 and R 7 may be absent.
  • the Group 15 metal-containing catalyst compound can be represented by the following formula (X).
  • Ph represents phenyl
  • the catalyst system may include a catalyst or catalyst component in a slurry, which may have an initial catalyst compound, and an added solution catalyst component that is added to the slurry.
  • the initial catalyst component slurry may have no catalysts. In this case, two or more solution catalysts may be added to the slurry to cause each to be supported.
  • the catalyst component slurry can include an activator and a support, or a supported activator.
  • the slurry can include a catalyst compound in addition to the activator and the support.
  • the catalyst compound in the slurry may be supported.
  • the slurry may include one or more activators and supports, and one more catalyst compounds.
  • the slurry may include two or more activators (such as alumoxane and a modified alumoxane) and a catalyst compound, or the slurry may include a supported activator and more than one catalyst compounds.
  • the slurry includes a support, an activator, and two catalyst compounds.
  • the slurry includes a support, an activator and two different catalyst compounds, which may be added to the slurry separately or in combination.
  • the slurry, containing silica and alumoxane may be contacted with a catalyst compound, allowed to react, and thereafter the slurry is contacted with another catalyst compound, for example, in a trim system.
  • the molar ratio of metal in the activator to metal in the pre-catalyst compound in the slurry may be may be 1000:1 to 0.5:1, 300:1 to 1:1, or 150:1 to 1:1.
  • the slurry can include a support material which may be any inert particulate carrier material known in the art, including, but not limited to, silica, fumed silica, alumina, clay, talc or other support materials such as disclosed above.
  • the slurry contains silica and an activator, such as methyl aluminoxane (“MAO”), modified methyl aluminoxane (“MMAO”), as discussed further below.
  • MAO methyl aluminoxane
  • MMAO modified methyl aluminoxane
  • One or more diluents or carriers can be used to facilitate the combination of any two or more components of the catalyst system in the slurry or in the trim catalyst solution.
  • the single site catalyst compound and the activator can be combined together in the presence of toluene or another non-reactive hydrocarbon or hydrocarbon mixture to provide the catalyst mixture.
  • other suitable diluents can include, but are not limited to, ethylbenzene, xylene, pentane, hexane, heptane, octane, other hydrocarbons, or any combination thereof
  • the support either dry or mixed with toluene can then be added to the catalyst mixture or the catalyst/activator mixture can be added to the support.
  • the terms “support” and “carrier” are used interchangeably and refer to any support material, including a porous support material, such as talc, inorganic oxides, and inorganic chlorides.
  • the one or more single site catalyst compounds of the slurry can be supported on the same or separate supports together with the activator, or the activator can be used in an unsupported form, or can be deposited on a support different from the single site catalyst compounds, or any combination thereof This may be accomplished by any technique commonly used in the art.
  • the single site catalyst compound can contain a polymer bound ligand.
  • the single site catalyst compounds of the slurry can be spray dried.
  • the support used with the single site catalyst compound can be functionalized.
  • the support can be or include one or more inorganic oxides, for example, of Group 2, 3, 4, 5, 13, or 14 elements.
  • the inorganic oxide can include, but is not limited to silica, alumina, titania, zirconia, boria, zinc oxide, magnesia, or any combination thereof.
  • Illustrative combinations of inorganic oxides can include, but are not limited to, alumina-silica, silica-titania, alumina-silica-titania, alumina-zirconia, alumina-titania, and the like.
  • the support can be or include alumina, silica, or a combination thereof. In one embodiment described herein, the support is silica.
  • Suitable commercially available silica supports can include, but are not limited to, ES757, ES70, and ES7OW available from PQ Corporation.
  • Suitable commercially available silica-alumina supports can include, but are not limited to, SIRAL® 1, SIRAL® 5, SIRAL® 10, SIRAL® 20, SIRAL® 28M, SIRAL® 30, and SIRAL® 40, available from SASOL®.
  • catalysts supports comprising silica gels with activators, such as methylaluminoxanes (MAOs), are used in the trim systems described, since these supports may function better for co-supporting solution carried catalysts.
  • Suitable supports may also be selected from the Cab-o-sil® materials available from Cabot Corporation and silica materials available from the Grace division of W.R. Grace & Company.
  • Catalyst supports may also include polymers that are covalently bonded to a ligand on the catalyst.
  • polymers that are covalently bonded to a ligand on the catalyst.
  • two or more catalyst molecules may be bonded to a single polyolefin chain.
  • the term “activator” may refer to any compound or combination of compounds, supported, or unsupported, which can activate a single site catalyst compound or component, such as by creating a cationic species of the catalyst component. For example, this can include the abstraction of at least one leaving group (the “X” group in the single site catalyst compounds described herein) from the metal center of the single site catalyst compound/component.
  • the activator may also be referred to as a “co-catalyst”.
  • the activator can include a Lewis acid or a non-coordinating ionic activator or ionizing activator, or any other compound including Lewis bases, aluminum alkyls, and/or conventional-type co-catalysts.
  • illustrative activators can include, but are not limited to, aluminoxane or modified aluminoxane, and/or ionizing compounds, neutral or ionic, such as Dimethylanilinium tetrakis(pentafluorophenyl)borate, Triphenylcarbenium tetrakis(pentafluorophenyl)borate, Dimethylanilinium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Triphenylcarbenium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Diphenylcarbenium tetrakis(3,5-(CF 3 ) 2 phenyl)borate, Diphen
  • activators may or may not bind directly to the support surface or may be modified to allow them to be bound to a support surface while still maintaining their compatability with the polymerization system.
  • tethering agents may be derived from groups that are reactive with surface hydroxyl species.
  • reactive functional groups that can be used to create tethers include aluminum halides, aluminum hydrides, aluminum alkyls, aluminum aryls, sluminum alkoxides, electrophilic silicon reagents, alkoxy silanes, amino silanes, boranes.
  • Aluminoxanes can be described as oligomeric aluminum compounds having —Al(R)—O— subunits, where R is an alkyl group.
  • aluminoxanes include, but are not limited to, methylaluminoxane (“MAO”), modified methylaluminoxane (“MMAO”), ethylaluminoxane, isobutylaluminoxane, or a combination thereof
  • Aluminoxanes can be produced by the hydrolysis of the respective trialkylaluminum compound.
  • MMAO can be produced by the hydrolysis of trimethylaluminum and a higher trialkylaluminum, such as triisobutylaluminum.
  • MMAOs are generally more soluble in aliphatic solvents and more stable during storage. There are a variety of methods for preparing aluminoxane and modified aluminoxanes.
  • a visually clear MAO can be used.
  • a cloudy or gelled aluminoxane can be filtered to produce a clear aluminoxane or clear aluminoxane can be decanted from a cloudy aluminoxane solution.
  • a cloudy and/or gelled aluminoxane can be used.
  • Another aluminoxane can include a modified methyl aluminoxane (“MMAO”) type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylaluminoxane type 3A).
  • a suitable source of MAO can be a solution having from about 1 wt. % to about a 50 wt. % MAO, for example.
  • Commercially available MAO solutions can include the 10 wt. % and 30 wt. % MAO solutions available from Albemarle Corporation, of Baton Rouge, La.
  • one or more organo-aluminum compounds such as one or more alkylaluminum compounds can be used in conjunction with the aluminoxanes.
  • alkylaluminum species that may be used are diethylaluminum ethoxide, diethylaluminum chloride, and/or diisobutylaluminum hydride.
  • trialkylaluminum compounds include, but are not limited to, trimethylaluminum, triethylaluminum (“TEAL”), triisobutylaluminum (“TiBAl”), tri-n-hexylaluminum, tri-n-octylaluminum, tripropylaluminum, tributylaluminum, and the like.
  • the catalyst component solution may include only a catalyst compound or may include an activator in addition to the catalyst compound.
  • the catalyst solution used in the trim process can be prepared by dissolving the catalyst compound and optional activators in a liquid solvent.
  • the liquid solvent may be an alkane, such as a C 5 to C 30 alkane, or a C 5 to C 10 alkane. Cyclic alkanes such as cyclohexane and aromatic compounds such as toluene may also be used.
  • mineral oil may be used as a solvent.
  • the solution employed should be liquid under the conditions of polymerization and relatively inert.
  • the liquid utilized in the catalyst compound solution is different from the diluent used in the catalyst component slurry.
  • the liquid utilized in the catalyst compound solution is the same as the diluent used in the catalyst component solution.
  • the ratio of metal in the activator to metal in the pre-catalyst compound in the solution may be may be 1000:1 to 0.5:1, 300:1 to 1:1, or 150:1 to 1:1. In certain cases, it may be advantageous to have an excess of catalyst compound such that the ratio is ⁇ 1:1, for example, 1:1 to 0.5:1 or 1:1 to 0.1:1 or 1:1 to 0.01.
  • the activator and catalyst compound is present in the solution at up to about 90 wt. %, at up to about 50 wt. %, at up to about 20 wt. %, preferably at up to about 10 wt. %, at up to about 5 wt. %, at less than 1 wt. %, or between 100 ppm and 1 wt. %, based upon the weight of the solvent and the activator or catalyst compound.
  • the catalyst component solution can comprise any one of the soluble catalyst compounds described in the catalyst section herein. As the catalyst is dissolved in the solution, a higher solubility is desirable. Accordingly, the catalyst compound in the catalyst component solution may often include a metallocene, which may have higher solubility than other catalysts.
  • any of the above described catalyst component containing solutions may be combined with any of the catalyst component containing slurry/slurries described above.
  • more than one catalyst component solution may be utilized.
  • a static control agent is a chemical composition which, when introduced into a fluidized bed reactor, may influence or drive the static charge (negatively, positively, or to zero) in the fluidized bed.
  • the specific static control agent used may depend upon the nature of the static charge, and the choice of static control agent may vary dependent upon the polymer being produced and the single site catalyst compounds being used.
  • Control agents such as aluminum stearate may be employed.
  • the static control agent used may be selected for its ability to receive the static charge in the fluidized bed without adversely affecting productivity.
  • Other suitable static control agents may also include aluminum distearate, ethoxlated amines, and anti-static compositions such as those provided by Innospec Inc. under the trade name OCTASTAT.
  • OCTASTAT 2000 is a mixture of a polysulfone copolymer, a polymeric polyamine, and oil-soluble sulfonic acid.
  • control agents may be employed either alone or in combination as a control agent.
  • a carboxylate metal salt may be combined with an amine containing control agent (e.g., a carboxylate metal salt with any family member belonging to the KEMAMINE® (available from Crompton Corporation) or ATMER® (available from ICI Americas Inc.) family of products).
  • an amine containing control agent e.g., a carboxylate metal salt with any family member belonging to the KEMAMINE® (available from Crompton Corporation) or ATMER® (available from ICI Americas Inc.) family of products).
  • the polyethyleneimines may be linear, branched, or hyperbranched (e.g., forming dendritic or arborescent polymer structures). They can be a homopolymer or copolymer of ethyleneimine or mixtures thereof (referred to as polyethyleneimine(s) hereafter). Although linear polymers represented by the chemical formula —[CH 2 —CH 2 —NH]— may be used as the polyethyleneimine, materials having primary, secondary, and tertiary branches can also be used. Commercial polyethyleneimine can be a compound having branches of the ethyleneimine polymer. Suitable polyethyleneimines are commercially available from BASF Corporation under the trade name Lupasol.
  • Another useful continuity additive can include a mixture of aluminum distearate and an ethoxylated amine-type compound, e.g., IRGASTAT AS-990, available from Huntsman (formerly Ciba Specialty Chemicals).
  • the mixture of aluminum distearate and ethoxylated amine type compound can be slurried in mineral oil e.g., Hydrobrite 380.
  • the mixture of aluminum distearate and an ethoxylated amine type compound can be slurried in mineral oil to have total slurry concentration of ranging from about 5 wt. % to about 50 wt. % or about 10 wt. % to about 40 wt. %, or about 15 wt. % to about 30 wt. %.
  • the continuity additive(s) or static control agent(s) may be added to the reactor in an amount ranging from 0.05 to 200 ppm, based on the weight of all feeds to the reactor, excluding recycle. In some embodiments, the continuity additive may be added in an amount ranging from 2 to 100 ppm, or in an amount ranging from 4 to 50 ppm.
  • FIG. 1 is a schematic of a gas-phase reactor system 100 , showing the addition of at least two catalysts, at least one of which is added as a trim catalyst.
  • the catalyst component slurry preferably a mineral oil slurry including at least one support and at least one activator, at least one supported activator, and optional catalyst compounds may be placed in a vessel or catalyst pot (cat pot) 102 .
  • the cat pot 102 is an agitated holding tank designed to keep the solids concentration homogenous.
  • a catalyst component solution, prepared by mixing a solvent and at least one catalyst compound and/or activator, is placed in another vessel, which can be termed a trim pot 104 .
  • the catalyst component slurry can then be combined in-line with the catalyst component solution to form a final catalyst composition.
  • a nucleating agent 106 such as silica, alumina, fumed silica or any other particulate matter may be added to the slurry and/or the solution in-line or in the vessels 102 or 104 .
  • additional activators or catalyst compounds may be added in-line.
  • a second catalyst slurry that includes a different catalyst may be introduced from a second cat pot. The two catalyst slurries may be used as the catalyst system with or without the addition of a solution catalyst from the trim pot.
  • the catalyst component slurry and solution can be mixed in-line.
  • the solution and slurry may be mixed by utilizing a static mixer 108 or an agitating vessel (not shown).
  • the mixing of the catalyst component slurry and the catalyst component solution should be long enough to allow the catalyst compound in the catalyst component solution to disperse in the catalyst component slurry such that the catalyst component, originally in the solution, migrates to the supported activator originally present in the slurry.
  • the combination forms a uniform dispersion of catalyst compounds on the supported activator forming the catalyst composition.
  • the length of time that the slurry and the solution are contacted is typically up to about 120 minutes, such as about 0.01 to about 60 minutes, about 5 to about 40 minutes, or about 10 to about 30 minutes.
  • the combination yield a new polymerization catalyst in less than 1 h, less than 30 min, or less than 15 min. Shorter times are more effective, as the new catalyst is ready before being introduces into the reactor, providing the potential for faster flow rates.
  • an aluminum alkyl, an ethoxylated aluminum alkyl, an aluminoxane, an anti-static agent or a borate activator such as a C 1 to C 15 alkyl aluminum (for example tri-isobutyl aluminum, trimethyl aluminum or the like), a C 1 to C 15 ethoxylated alkyl aluminum or methyl aluminoxane, ethyl aluminoxane, isobutylaluminoxane, modified aluminoxane or the like are added to the mixture of the slurry and the solution in line.
  • the alkyls, antistatic agents, borate activators and/or aluminoxanes may be added from an alkyl vessel 110 directly to the combination of the solution and the slurry, or may be added via an additional alkane (such as isopentane, hexane, heptane, and or octane) carrier stream, for example, from a hydrocarbon vessel 112 .
  • the additional alkyls, antistatic agents, borate activators and/or aluminoxanes may be present at up to about 500 ppm, at about 1 to about 300 ppm, at 10 to about 300 ppm, or at about 10 to about 100 ppm.
  • Carrier streams that may be used include isopentane and or hexane, among others.
  • the carrier may be added to the mixture of the slurry and the solution, typically at a rate of about 0.5 to about 60 lbs/hr (27 kg/hr) or greater, depending on reactor size.
  • a carrier gas 114 such as nitrogen, argon, ethane, propane and the like, may be added in-line to the mixture of the slurry and the solution.
  • the carrier gas may be added at the rate of about 1 to about 100 lb/hr (0.4 to 45 kg/hr), or about 1 to about 50 lb/hr (5 to 23 kg/hr), or about 1 to about 25 lb/hr (0.4 to 11 kg/hr).
  • a liquid carrier stream is introduced into the combination of the solution and slurry that is moving in a downward direction.
  • the mixture of the solution, the slurry and the liquid carrier stream may pass through a mixer or length of tube for mixing before being contacted with a gaseous carrier stream.
  • a comonomer 116 such as hexene, another alpha-olefin or diolefin, may be added in-line to the mixture of the slurry and the solution.
  • the slurry/solution mixture is then passed through an injection tube 118 to a reactor 120 .
  • a nucleating agent 122 such as fumed silica, can be added directly into the reactor 120 .
  • the injection tube may aerosolize the slurry/solution mixture. Any number of suitable tubing sizes and configurations may be used to aerosolize and/or inject the slurry/solution mixture.
  • a gas stream 124 such as cycle gas, or re-cycle gas 126 , monomer, nitrogen, or other materials is introduced into a support tube 128 that surrounds the injection tube 118 .
  • oxygen or fluorobenzene can be added to the reactor 120 directly or to the gas stream 124 to control the polymerization rate.
  • a metallocene catalyst which is sensitive to oxygen or fluorobenzene
  • oxygen can be used to modify the metallocene polymerization rate relative to the polymerization rate of the other catalyst.
  • An example of such a catalyst combination is bis(n-propyl cyclopentadienyl)zirconium dichloride and [(2,4,6-Me 3 C 6 H 2 )NCH 2 CH 2 ] 2 NHZrBn 2 , where Me is methyl or bis(indenyl)zirconium dichloride and [(2,4,6-Me 3 C 6 H 2 )NCH 2 CH 2 ] 2 NHHfBn 2 , where Me is methyl.
  • the contact temperature of the slurry and the solution is in the range of from 0° C. to about 80° C., from about 0° C. to about 60° C., from about 10° C., to about 50° C. and from about 20° C. to about 40° C.
  • a slurry can be combined with two or more solutions having the same or different catalyst compounds and or activators.
  • the solution may be combined with two or more slurries each having the same or different supports, and the same or different catalyst compounds and or activators.
  • two or more slurries combined with two or more solutions, preferably in-line where the slurries each comprise the same or different supports and may comprise the same or different catalyst compounds and or activators and the solutions comprise the same or different catalyst compounds and or activators.
  • the slurry may contain a supported activator and two different catalyst compounds, and two solutions, each containing one of the catalysts in the slurry, are each independently combined, in-line, with the slurry.
  • the properties of the product polymer may be controlled by adjusting the timing, temperature, concentrations, and sequence of the mixing of the solution, the slurry and any optional added materials (nucleating agents, catalyst compounds, activators, etc) described above.
  • the MWD, composition distribution, melt index, relative amount of polymer produced by each catalyst, and other properties of the polymer produced may also be changed by manipulating process parameters. Any number of process parameters may be adjusted, including manipulating hydrogen concentration in the polymerization system, changing the amount of the first catalyst in the polymerization system, changing the amount of the second catalyst in the polymerization system. Other process parameters that can be adjusted include changing the relative ratio of the catalyst in the polymerization process (and optionally adjusting their individual feed rates to maintain a steady or constant resin production rate).
  • the concentrations of reactants in the reactor 120 can be adjusted by changing the amount of liquid or gas that is withdrawn or purged from the process, changing the amount and/or composition of a recovered liquid and/or recovered gas returned to the polymerization process, wherein the recovered liquid or recovered gas can be recovered from polymer discharged from the polymerization process.
  • Further concentration parameters that can be adjusted include changing the polymerization temperature, changing the ethylene partial pressure in the polymerization process, changing the ethylene to comonomer ratio in the polymerization process, changing the activator to transition metal ratio in the activation sequence.
  • Time dependant parameters may be adjusted, such as changing the relative feed rates of the slurry or solution, changing the mixing time, the temperature and or degree of mixing of the slurry and the solution in-line, adding different types of activator compounds to the polymerization process, and adding oxygen or fluorobenzene or other catalyst poison to the polymerization process. Any combinations of these adjustments may be used to control the properties of the final polymer product.
  • the composition distribution of the polymer product is measured at regular intervals and one of the above process parameters, such as temperature, catalyst compound feed rate, the ratio of the two or more catalysts to each other, the ratio of comonomer to monomer, the monomer partial pressure, and or hydrogen concentration, is altered to bring the composition to the desired level, if necessary.
  • the composition distribution may be performed by temperature rising elution fractionation (TREF), or similar techniques TREF measures composition as a function of elution temperature.
  • a polymer product property is measured in-line and in response the ratio of the catalysts being combined is altered.
  • the molar ratio of the catalyst compound in the catalyst component slurry to the catalyst compound in the catalyst component solution, after the slurry and solution have been mixed to form the final catalyst composition is 500:1 to 1:500, or 100:1 to 1:100, or 50:1 to 1:50, or 10:1 to 1:10, or 5:1 to 1:5.
  • the molar ratio of a Group 15 catalyst compound in the slurry to a ligand metallocene catalyst compound in the solution, after the slurry and solution have been mixed to form the catalyst composition is 500:1, 100:1, 50:1, 10:1, 5:1, 1:5, 1:10, 1:100, or 1:500.
  • the product property measured can include the polymer product's flow index, melt index, density, MWD, comonomer content, composition distribution, and combinations thereof.
  • the processes described herein immobilize the solution catalyst compound in and on a support, preferably a supported activator.
  • the in-line immobilization techniques described herein preferably result in a supported catalyst system that when introduced to the reactor provides for suitable polymer properties, with appropriate particle morphology, bulk density, or higher catalyst activities and without the need for additional equipment in order to introduce catalyst compound solution into a reactor, particularly a gas phase or slurry phase reactor.
  • the catalyst system can be used to polymerize one or more olefins to provide one or more polymer products therefrom.
  • Any suitable polymerization process can be used, including, but not limited to, high pressure, solution, slurry, and/or gas phase polymerization processes.
  • modifications to a catalyst addition system that are similar to those discussed with respect to FIG. 1 can be used.
  • a trim system may be used to feed catalyst to a loop slurry reactor for polyethylene copolymer production.
  • polyethylene and “polyethylene copolymer” refer to a polymer having at least 50 wt. % ethylene-derived units.
  • the polyethylene can have at least 70 wt. % ethylene-derived units, at least 80 wt. % ethylene-derived units, at least 90 wt. % ethylene-derived units, at least 95 wt. % ethylene-derived units, or 100 wt. % ethylene-derived units.
  • the polyethylene can, thus, be a homopolymer or a copolymer, including a terpolymer, having one or more other monomeric units.
  • a polyethylene can include, for example, at least one or more other olefins or comonomers.
  • Suitable comonomers can contain 3 to 16 carbon atoms, from 3 to 12 carbon atoms, from 4 to 10 carbon atoms, and from 4 to 8 carbon atoms.
  • Examples of comonomers include, but are not limited to, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 4-methylpent-l-ene, 1-decene, 1-dodecene, 1-hexadecene, and the like.
  • small amounts of diene monomers, such as 1,7-octadiene may be added to the polymerization to adjust polymer properties.
  • the fluidized bed reactor 120 can include a reaction zone 130 and a velocity reduction zone 132 .
  • the reaction zone 130 can include a bed 134 that includes growing polymer particles, formed polymer particles and a minor amount of catalyst particles fluidized by the continuous flow of the gaseous monomer and diluent to remove heat of polymerization through the reaction zone.
  • some of the re-circulated gases 124 can be cooled and compressed to form liquids that increase the heat removal capacity of the circulating gas stream when readmitted to the reaction zone.
  • a suitable rate of gas flow can be readily determined by experimentation.
  • Make-up of gaseous monomer to the circulating gas stream can be at a rate equal to the rate at which particulate polymer product and monomer associated therewith is withdrawn from the reactor and the composition of the gas passing through the reactor can be adjusted to maintain an essentially steady state gaseous composition within the reaction zone.
  • the gas leaving the reaction zone 130 can be passed to the velocity reduction zone 132 where entrained particles are removed, for example, by slowing and falling back to the reaction zone 130 . If desired, finer entrained particles and dust can be removed in a separation system 136 , such as a cyclone and/or fines filter.
  • the gas 124 can be passed through a heat exchanger 138 where at least a portion of the heat of polymerization can be removed. The gas can then be compressed in a compressor 140 and returned to the reaction zone 130 .
  • the reactor temperature of the fluid bed process can be greater than about 30° C., about 40° C., about 50° C., about 90° C., about 100° C., about 110° C., about 120° C., about 150° C., or higher.
  • the reactor temperature is operated at the highest feasible temperature taking into account the sintering temperature of the polymer product within the reactor.
  • Preferred reactor temperatures are between 70 and 95° C. More preferred reactor temperatures are between 75 and 90° C.
  • the upper temperature limit in one embodiment is the melting temperature of the polyethylene copolymer produced in the reactor.
  • higher temperatures may result in narrower MWDs, which can be improved by the addition of the MCN, or other, co-catalysts, as described herein.
  • Hydrogen gas can be used in olefin polymerization to control the final properties of the polyolefin.
  • increasing concentrations (partial pressures) of hydrogen can increase the flow index (FI) of the polyethylene copolymer generated.
  • the flow index can thus be influenced by the hydrogen concentration.
  • the amount of hydrogen in the polymerization can be expressed as a mole ratio relative to the total polymerizable monomer, for example, ethylene, or a blend of ethylene and hexene or propylene.
  • the amount of hydrogen used in the polymerization process can be an amount necessary to achieve the desired flow index of the final polyolefin resin.
  • the mole ratio of hydrogen to total monomer (H 2 :monomer) can be greater than about 0.0001, greater than about 0.0005, or greater than about 0.001.
  • the mole ratio of hydrogen to total monomer (H 2 :monomer) can be less than about 10, less than about 5, less than about 3, and less than about 0.10.
  • a desirable range for the mole ratio of hydrogen to monomer can include any combination of any upper mole ratio limit with any lower mole ratio limit described herein.
  • the amount of hydrogen in the reactor at any time can range to up to about 5,000 ppm, up to about 4,000 ppm in another embodiment, up to about 3,000 ppm, or between about 50 ppm and 5,000 ppm, or between about 50 ppm and 2,000 ppm in another embodiment.
  • the amount of hydrogen in the reactor can range from a low of about 1 ppm, about 50 ppm, or about 100 ppm to a high of about 400 ppm, about 800 ppm, about 1,000 ppm, about 1,500 ppm, or about 2,000 ppm.
  • the ratio of hydrogen to total monomer (H 2 :monomer) can be about 0.00001:1 to about 2:1, about 0.005:1 to about 1.5:1, or about 0.0001:1 to about 1:1.
  • the one or more reactor pressures in a gas phase process can vary from 690 kPa (100 psig) to 3,448 kPa (500 psig), in the range from 1,379 kPa (200 psig) to 2,759 kPa (400 psig), or in the range from 1,724 kPa (250 psig) to 2,414 kPa (350 psig).
  • the gas phase reactor can be capable of producing from about 10 kg of polymer per hour (25 lbs/hr) to about 90,900 kg/hr (200,000 lbs/hr), or greater, and greater than about 455 kg/hr (1,000 lbs/hr), greater than about 4,540 kg/hr (10,000 lbs/hr), greater than about 11,300 kg/hr (25,000 lbs/hr), greater than about 15,900 kg/hr (35,000 lbs/hr), and greater than about 22,700 kg/hr (50,000 lbs/hr), and from about 29,000 kg/hr (65,000 lbs/hr) to about 45,500 kg/hr (100,000 lbs/hr).
  • a slurry polymerization process can also be used in embodiments.
  • a slurry polymerization process generally uses pressures in the range of from about 101 kPa (1 atmosphere) to about 5,070 kPa (50 atmospheres) or greater, and temperatures in the range of from about 0° C. to about 120° C., and more particularly from about 30° C. to about 100° C.
  • a suspension of solid, particulate polymer can be formed in a liquid polymerization diluent medium to which ethylene, comonomers, and hydrogen along with catalyst can be added.
  • the suspension including diluent can be intermittently or continuously removed from the reactor where the volatile components are separated from the polymer and recycled, optionally after a distillation, to the reactor.
  • the liquid diluent employed in the polymerization medium can be an alkane having from 3 to 7 carbon atoms, such as, for example, a branched alkane.
  • the medium employed should be liquid under the conditions of polymerization and relatively inert. When a propane medium is used the process should be operated above the reaction diluent critical temperature and pressure. In one embodiment, a hexane, isopentane, or isobutane medium can be employed.
  • the slurry can be circulated in a continuous loop system.
  • the product polyethylene can have a melt index ratio (MIR or I 21 /I 2 ) ranging from about 5 to about 300, or from about 10 to less than about 150, or, in many embodiments, from about 15 to about 50.
  • Flow index (FI, HLMI, or I 21 can be measured in accordance with ASTM D1238 (190° C., 21.6 kg).
  • the melt index (MI, I 2 ) can be measured in accordance with ASTM D1238 (at 190° C., 2.16 kg weight).
  • Density can be determined in accordance with ASTM D-792. Density is expressed as grams per cubic centimeter (g/cm 3 ) unless otherwise noted.
  • the polyethylene can have a density ranging from a low of about 0.89 g/cm 3 , about 0.90 g/cm 3 , or about 0.91 g/cm 3 to a high of about 0.95 g/cm 3 , about 0.96 g/cm 3 , or about 0.97 g/cm 3 .
  • the polyethylene can have a bulk density, measured in accordance with ASTM D1895 method B, of from about 0.25 g/cm 3 to about 0.5 g/cm 3 .
  • the bulk density of the polyethylene can range from a low of about 0.30 g/cm 3 , about 0.32 g/cm 3 , or about 0.33 g/cm 3 to a high of about 0.40 g/cm 3 , about 0.44 g/cm 3 , or about 0.48 g/cm 3 .
  • the polyethylene can be suitable for such articles as films, fibers, nonwoven and/or woven fabrics, extruded articles, and/or molded articles.
  • films include blown or cast films formed by coextrusion or by lamination useful as shrink film, cling film, stretch film, sealing films, oriented films, snack packaging, heavy duty bags, grocery sacks, baked and frozen food packaging, medical packaging, industrial liners, membranes, etc. in food-contact and non-food contact applications, agricultural films and sheets.
  • fibers include melt spinning, solution spinning and melt blown fiber operations for use in woven or non-woven form to make filters, diaper fabrics, hygiene products, medical garments, geotextiles, etc.
  • extruded articles examples include tubing, medical tubing, wire and cable coatings, pipe, geomembranes, and pond liners.
  • molded articles include single and multi-layered constructions in the form of bottles, tanks, large hollow articles, rigid food containers and toys, etc.
  • SCB short chain branching
  • LCB long chain branching
  • shorter chains lowers the melt temperature of the polymer, and may enhance the processability.
  • SCB on shorter chains may force these chains out of crystallites and into amorphous regions, lowering the toughness of the resulting polymer product.
  • Hydrogen may be added to the polymer reactions to control molecular weight.
  • the hydrogen acts as chain termination agent, essentially replacing a monomer or comonomer molecule in the reaction. This stops the formation of a current polymer chain, and allows a new polymer chain to begin.
  • the catalysts A-J shown in Table 1 were prepared as described below. All the catalysts prepared were screened in a fluidized bed reactor equipped with devices for temperature control, catalyst feeding or injection equipment, gas chromatograph (GC) analyzer for monitoring and controlling monomer and comonomer gas feeds and equipment for polymer sampling and collecting.
  • the reactor consisted of a 6 inch (15.24 cm) diameter bed section increasing to 10 inches (25.4 cm) at the reactor top. Gas comes in through a perforated distributor plate allowing fluidization of the bed contents and polymer sample is discharged at the reactor top.
  • the comonomer in the example polymerizations herein is 1-hexene.
  • the polymerization parameters are outlined in the table 1 below and plotted in FIGS. 2 and 3 .
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity 1-2 ft/sec (0.3 to 0.6 m/sec).
  • the reactor was operated at a temperature of 175 F (79 C) and total pressure of 300 psig (2274 kPa gauge) including 35 mol % ethylene.
  • FIG. 2 is a plot 200 of a series of polymers that were prepared to test the relative abilities of a series of metallocene catalysts to prepare a resin having about a 1 melt index (MI) and a density (D) of about 0.92.
  • the polymerizations were performed in the continuous gas phase reactor (LGPR) described above.
  • the left axis 202 represents the gas-phase ratios of hydrogen to ethylene monomer (H 2 /C 2 ) used to achieve the target properties, in units of parts-per-million (mol) of H 2 per mol % C 2 (ppm/mol %).
  • the right axis 204 represents the comonomer to ethylene ratio (C 6 /C 2 ) used to achieve the target properties, in units of mol per mol.
  • Comparing C 6 /C 2 levels used to achieve the property targets indicate the relative abilities of the catalysts to incorporate comonomer. For example, comparing the C 6 /C 2 level 206 for (1-EtInd) 2 ZrCl 2 (B) to the C 6 /C 2 level 208 for (PrCp) 2 HfF 2 (I) gives a ratio of about 36/9 or about four. This indicates that for a given C 6 /C 2 gas ratio, a polymer prepared with (PrCp) 2 HfF 2 will have approximately four times the short chain branching (SCB) of a polymer prepared using (1-EtInd) 2 ZrCl 2 .
  • SCB short chain branching
  • This data is useful for controlling composition distributions of polymers made as in-situ blends using catalyst mixtures, for example, as co-supported catalysts on a single support.
  • the data is also useful for determining which catalysts should be combined to have a composition distribution containing both comonomer rich (low density) and comonomer poor (high density) components.
  • FIG. 3 is a plot 300 of the series of polymers of FIG. 2 , showing the melt index ratio (MIR) of the series of polymers made by different metallocene (MCN) catalysts.
  • MIR melt index ratio
  • MFR melt flow ratio
  • I 21 /I 2 interchangeably refer to the ratio of the flow index (“FI” or “I 21 ”) to the melt index (“MI” or “I 2 ”).
  • the MI (I 2 ) can be measured in accordance with ASTM D1238 (at 190° C., 2.16 kg weight).
  • the FI (I 21 ) can be measured in accordance with ASTM D1238 (at 190° C., 21.6 kg weight).
  • ASTM D1238 at 190° C., 2.16 kg weight
  • FI I 21
  • Like numbered items are as described with respect to FIG. 2 .
  • the left axis 302 represents the MIR.
  • the MIR (which may also be termed melt flow ratio or MFR) is the ratio of the I21 and I2 melt indices and may indicate the presence of long chain branching. For linear resins, without LCB, the ratio is around 25 or less. Higher MIR values may indicate the presence of LCB which can be detrimental to film properties, as noted above.
  • the highest MIR ratio 304 was for (CH 2 ) 3 Si(CpMe 4 )CpZrCl 2 (J), indicating that polymer produced by this catalyst has the most LCB. In contrast, blending resins for with the two different catalysts forms a final product that will have a higher MIR.
  • catalysts were selected to determine the dependence of the molecular weight (Mw) on the H 2 ratio.
  • These catalysts included three catalysts that generate lower Mw polyethylene, (CpMe 5 )(1-MeInd)ZrCl 2 (A) 306 , (1-EtInd) 2 ZrCl 2 (B) 308 , and (Me 4 Cp)(1,3-Me 2 Ind)Zr Cl 2 (E) 310 .
  • the catalysts also included a catalyst that generates a middle Mw polyethylene, (PrCp) 2 HfF 2 (I) 312 .
  • Table 2 contains data on the dependence of Mw on H 2 /C 2 level.
  • the equations from Table 3 can be used to predict the amounts of (1-EtInd) 2 ZrCl 2 needed in a combination with the catalyst (PrCp) 2 HfF 2 to make an overall resin with Mw of 100 Kg/mol at four different H 2 levels. These values may be used to set initial control points, for example, if (PrCp) 2 HfF 2 is used as a supported catalyst component, and (1-EtInd) 2 ZrCl 2 is a solution catalyst component, to be added as a trim catalyst. In this embodiment, the amount of the (1-EtInd) 2 ZrCl 2 catalyst that is added may be controlled to achieve Mw and other performance targets. Results for various combinations are shown in Table 4.
  • HfP is capable of polymerizing ethylene and mixtures of ethylene and comonomers in the presence of an activator and a support, a cocatalyst, or both.
  • the activator and support may be the same or different. Multiple activators, supports and or cocatalysts may be used simultaneously. Cocatalysts may be added to modify any of the ingredients.
  • the descriptor catalyst, HfP, activator, supports and or cocatalysts refers to the actual compounds and also solutions of these compounds in hydrocarbon solvents.
  • the catalysts should be soluble in alkane solvents such as hexane, paraffinic solvents, and mineral oil.
  • alkane solvents such as hexane, paraffinic solvents, and mineral oil.
  • the solubility may be greater than 0.0001 wt. %, greater than 0.01 wt. %, greater than 1 wt. %, or greater than 2%.
  • Toluene may also be used as a solvent as the catalyst may be more soluble in an aromatic solvent
  • a combination of HfP, an activator (MAO), and a support (silica) was reacted with trim catalysts in hydrocarbon solvents to yield a polymerization catalyst with a different polymerization behavior than expected from the combination of the individual components. More specifically, the molecular weight distribution for a polymer generated by the co-supported co-catalysts is broader than can be achieved by mixtures of polymers formed from the individual component catalysts. This change in polymerization behavior is exemplified by changes in the MWD, the CD, or MWD and CD of polymers formed by the mixture of HfP and the selected cocatalysts. Thus, combining catalysts, HfP, activator and optionally a support, additional cocatalysts, or both, in hydrocarbon solvents in an in-line mixer immediately prior to a polymerization reactor yields a new polymerization catalyst.
  • any sequence of the combination of catalysts, HfP, activator and optionally a support, additional cocatalysts, or both, in hydrocarbon solvents may be used.
  • the catalysts may be added to a mixture that includes HfP, activator and optionally a support, additional cocatalysts, or both.
  • catalysts and cocatalysts may be added to a mixture of ⁇ HfP, activator and optionally a support ⁇ .
  • catalysts and HfP may be added to a mixture that includes ⁇ activator and optionally a support and cocatalysts ⁇ .
  • catalysts HfP, the activator and optionally a support, additional cocatalysts or both, in hydrocarbon solvents then obtain a dry catalyst from the mixture.
  • This dry mixture may be fed directly, or as a slurry, into a polymerization reactor.
  • the change in the MWD and CD upon using the catalysts and HfP can be controlled by changing the ratio of the catalysts to HfP.
  • the MWD and CD is that of HfP.
  • the MWD and CD is that generated by the catalysts themselves.
  • Changing the ratio of catalysts changes the MWD and CD from that of the parents. The ratio can be changed to target specific MWD and CD targets.
  • Catalysts can be chosen to control the change in MWD or CD of the polymer formed. Employing catalysts that yield lower or higher molecular weight polymers than HfP will broaden the molecular weight distribution.
  • the response of the Mw of polymers made from the single components versus H2/C2 can be used as a guide for the selection. For example, a catalyst having less response to hydrogen than HfP will yield a higher Mw than a polymer produced by HfP by itself, as shown in FIG. 2 . Further, a catalyst having a higher response to hydrogen than HfP will, in a combination with HfP, yield a lower Mw than HfP by itself.
  • catalysts may be selected to change the composition distribution. For example, employing catalysts that incorporate less or more comonomer than HfP will broaden the composition distribution.
  • a rough guide to this effect is the relative gas C6/C2 ratios required to prepare an approximately 0.92 D resin from different catalysts. Those catalysts that give larger differences in C6/C2 gas ratios from HfP will broaden the CD more.
  • Molecular weight distributions can also be changed by employing a catalyst that yields a different MWD but similar average molecular weight to that from HfP.
  • the combination of catalysts with HfP can yield a MWD that is larger than expected from the theoretical combination of the individual catalysts.
  • Desirable materials based on an HfP base catalyst are made when the Mw and comonomer incorporation abilities of the catalysts are both higher than HfP.
  • desirable materials are also formed when the Mw and comonomer incorporation abilities of the catalysts are both lower than HfP.
  • desirable materials are made when the Mw and of the catalysts are similar to and the comonomer incorporation abilities lower than HfP.
  • FIG. 4 is a flow chart of a method 400 for making a co-supported polymerization catalyst.
  • the method 400 begins at block 402 with the generation of a plot of hydrogen/ethylene ratio versus the reciprocal of molecular weight of a polymer generated by each one of a number of catalysts. As discussed herein, the slope of each plot indicates the response of the corresponding catalyst to a hydrogen level.
  • a value is determined for the comonomer/ethylene ratio for each of the catalysts that can be used to achieve a single target density, such as 0.92.
  • the value of the ratio used to achieve the target density indicates the ability of the catalyst to incorporate comonomer.
  • a first catalyst is selected for the co-supported polymerization catalyst.
  • the first catalyst can be a commonly used commercial catalyst, or may be selected to have a low or a high ability to incorporate comonomer and a high or low response to hydrogen.
  • a second catalyst is selected for the co-supported polymerization catalyst.
  • the second catalyst can be selected to have a slope of the plot for the hydrogen/ethylene ratio versus the reciprocal of molecular weight that is at least about 1.5 times as large as the slope of the plot for the first catalyst. Further, the second catalyst can be selected to have a value for the comonomer/ethylene ratio that is less than about 0.5 as large as comonomer/ethylene ratio of the first catalyst.
  • the first catalyst and the second catalyst can be co-supported on a single support to create the co-supported polymerization catalyst, for example, using the trim techniques described herein, among others.
  • the solid was isolated by filtration, washed with cold pentane (2 ⁇ 50 mL) and dried under vacuum to give 29.2 g solid with a rac/meso ration of 0.94:1.
  • the isolated solid was extracted with warm hexane (ca. 150 mL) filtered away from a small amount of pink solid. The volume was reduced to about 125 mL and the solution was treated with trimethylsilylchloride (2.0 mL). The solution was filtered, concentrated to about 100 mL, heated to re-dissolve the precipitated product and allowed to cool slowly. After sitting overnight, the flask was cooled to ⁇ 20 C which caused some pink solid to precipitate. The flask was warmed to 55° C.
  • iodomethane (2.0 ml, 32.1 mmol) was dissolved in 80 ml dry diethyl ether in a 250 ml round bottom flask with magnetic spinbar. Flask was placed in a isohexane cold bath ( ⁇ 25° C.) in a wide mouth dewar. In a separate 100 ml Erlenmeyer flask, a room temperature solution of 1-methylindenyl lithium (3.50 g, 25.7 mmol) was prepared in 50 ml dry diethyl ether, affording a yellow solution. Slow, dropwise addition of indenyl lithium solution to the cold, stirred solution of iodomethane was performed over 15 min.
  • Ineos ES757 silica (3969 g) was charged into a dehydrator (6 ft length, 6.25 in diameter) equipped with a 3-zone heater then fluidized with dry N2 gas at a flow rate of 0.12 ft 3 /s. Afterwards, the temperature was raised to 200° C. in a 2 h period. After holding at 200° C. for 2 h, the temperature was raised to 610° C. in a 6 h period. After holding at 610° C. for 4 h, the temperature was allowed to cool to ambient temperature over a 12 h period. The silica was transferred under N 2 to an APC can then stored under N 2 pressure (20 psig).
  • a 2 L autoclave Under a N 2 atmosphere, a 2 L autoclave was charged with dry salt (200 g) and SMAO (3 g). At a pressure of 2 psig N 2 , dry, degassed 1-hexene (see Table 6) was added to the reactor with a syringe. The reactor was sealed, heated to 80° C. while stirring the bed, then charged with N 2 to a pressure of 20 psig. Then, solid catalyst was injected into the reactor with ethylene at a pressure of 220 psig; ethylene flow was allowed over the course of the run. The temperature was raised to 85° C. Hexene was fed into the reactor as a ratio to ethylene flow (0.08 g/g).
  • Hydrogen was fed into the reactor as a ratio to ethylene flow per the description in the table.
  • the hydrogen and ethylene ratios were measured by on-line GC analysis. Polymerizations were halted after 1 h by venting the reactor, cooling to room temperature then exposing to air. The salt was removed by stirring the crude product in water. The polymer was obtained by filtration then drying in a vacuum oven.
  • the two 75/25 batches were combined in a 4 L Nalgene bottle and manually mixed by spinning and shaking the bottle.
  • the two 50/50 batches were also mixed in the same manner.
  • the feed stock slurry was prepared by first adding 10 wt % MAO (24.7 lbs), toluene (35.8 lbs) and Cabosil TS-610 (3.4 lbs) to a 10 gallon feed tank. The mixture was stirred overnight at room temperature. HfP (III) (28.75 g, 0.06798 mol) was added then the resulting slurry was mixed for another hour at ⁇ 38-40° C. before spraying. The catalyst was spray dried at a slurry feed rate of 93 lb/h, 90% atomizer speed, and outlet temperature of 80° C. in a procedure similar to reported in U.S. Pat. No. 7,276,566 B2. Yield was 2289 g (85%). Analytical data are reported in Table 9.
  • the polymerization was conducted in a continuous gas phase fluidized bed reactor having a straight section of 24 inch (61 cm) diameter with a length of approximately 11.75 feet (3.6 m) and an expanded section of 10.2 feet (3.1 m) length and 4.2 feet (1.3 m) diameter at the largest width.
  • the fluidized bed is made up of polymer granules.
  • the gaseous feed streams of ethylene and hydrogen together with liquid 1-hexene were mixed together in a mixing tee arrangement and introduced below the reactor bed into the recycle gas line.
  • the individual flow rates of ethylene, hydrogen and 1-hexene were controlled to maintain fixed composition targets.
  • the ethylene concentration was controlled to maintain a constant ethylene partial pressure.
  • They hydrogen was controlled to maintain a constant hydrogen to ethylene mole ratio.
  • the concentrations of all gasses were measured by an on-line gas chromatograph to ensure relatively constant composition in the recycle gas stream.
  • the solid catalyst was injected directly into the fluidized bed using purified nitrogen as a carrier. Its rate of injection was adjusted to maintain a constant production rate of the polymer.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity 1-3 ft/sec (0.3 to 0.9 m/sec).
  • the reactor was operated at a total pressure of 300 psig (2068 kPa gauge). To maintain a constant reactor temperature, the temperature of the recycle gas was continuously adjusted up or down to accommodate any changes in the rate of heat generation due to the polymerization.
  • a solution of anti-static agents in hexane (1:1 Aluminum stearate: N-nonyldiethanolamine at 20 wt %) was fed into the reactor using a mixture of iso-pentane and nitrogen at such a rate as too maintain ca. 30 ppm anti-static agents in the fluidized bed.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the product was removed semi-continuously via a series of valves into a fixed volume chamber, which was simultaneously vented back to the reactor to allow highly efficient removal of the product, while at the same time recycling a large portion of the unreacted gases back to the reactor, This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen to deactivate any trace quantities of residual catalyst and cocatalyst.
  • a gas phase fluidized bed reactor of 0.35 meters internal diameter and 2.3 meters in bed height was utilized for polymerizations, with the results shown in Table 11.
  • the fluidized bed was made up of polymer granules and the gaseous feed streams of ethylene and hydrogen together with liquid 1-hexene comonomer were introduced below the reactor bed into the recycle gas line.
  • the individual flow rates of ethylene, hydrogen and 1-hexene were controlled to maintain fixed composition targets.
  • the ethylene concentration was controlled to maintain a constant ethylene partial pressure.
  • the hydrogen was controlled to maintain constant hydrogen to ethylene mole ratio.
  • the concentrations of all the gases were measured by an on-line gas chromatograph to ensure relatively constant composition in the recycle gas stream.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by the continuous flow of the make-up feed and recycle gas through the reaction zone. A superficial gas velocity of 0.6-0.9 meters/sec was used to achieve this.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the polymer production rate was in the range of 15-25 kg/hour.
  • the product was removed semi-continuously via a series of valves into a fixed volume chamber. This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen to deactivate any trace quantities of residual catalyst.
  • the solid catalyst was dispersed in degassed and dried mineral oil as a nominal 18 wt % slurry and contacted with the trim catalyst solution for a few seconds to minutes before being injected directly into the fluidized bed using purified nitrogen and isopentane as carriers in a manner that produces an effervescence of nitrogen in the liquid and spray to aid in dispersing the catalyst.
  • the trim catalyst was provided initially as a solution, and substantially diluted with isopentane to a concentration of about 0.015 wt % before being mixed in-line with the slurry catalyst component in a continuous manner prior to injection to the reactor.
  • the relative feeds of the slurry catalyst and the trim catalyst were controlled to achieve an aim target feed ratio of their active polymerization metals, and the feeds adjusted accordingly for overall polymer production rate and the relative amounts of polymer produced by each catalyst based somewhat on polymer flow index MFR and density, while also manipulating reaction temperature and the gas compositions in the reactor.
  • the reacting bed of growing polymer particles was maintained in a fluidized state by continually flowing the makeup feed and recycle gas through the reaction zone at a superficial gas velocity in about the range of 2.0 to 2.2 ft/sec (0.61 to 0.67 m/sec).
  • the reactor was operated at a total pressure of about 350 psig (2413 kPa gauge).
  • the temperature of the recycle gas was continuously adjusted up or down by passing the recirculating gas through the tubes of a shell-and-tube heat exchanger with cooling water on the shell-side to accommodate any changes in the rate of heat generation due to the polymerization.
  • a slurry mixture of anti-static agents in degassed and dried mineral oil (1:1 Aluminum stearate: N-nonyldiethanolamine at 20 wt % concentration) was fed into the reactor using a mixture of iso-pentane and nitrogen at such a rate as to achieve a concentration of between 38 and 123 ppmw anti-static agents in the fluidized bed.
  • Isopentane and/or nitrogen was optionally employed to assist in conveying and dispersing the slurry mixture of anti-static into the reactor fluidized bed via a 1 ⁇ 8 inch to 3/16 inch OD injection tube thief extending a few inches into the bed from the reactor side wall.
  • the fluidized bed was maintained at a constant height by withdrawing a portion of the bed at a rate equal to the rate of formation of particulate product.
  • the product was removed semi-continuously via a series of valves into a fixed volume discharge chamber. This product was purged to remove entrained hydrocarbons and treated with a small stream of humidified nitrogen immediately on discharge to a receiving fiberpak drum to deactivate any trace quantities of residual catalyst and cocatalyst.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
  • Polymerisation Methods In General (AREA)
  • Catalysts (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Compositions Of Macromolecular Compounds (AREA)
  • Polymerization Catalysts (AREA)
US15/117,363 2014-02-11 2015-02-10 Producing polyolefin products Abandoned US20160347890A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US15/117,363 US20160347890A1 (en) 2014-02-11 2015-02-10 Producing polyolefin products

Applications Claiming Priority (11)

Application Number Priority Date Filing Date Title
US201461938466P 2014-02-11 2014-02-11
US201461938472P 2014-02-11 2014-02-11
US201461981291P 2014-04-18 2014-04-18
US201461985151P 2014-04-28 2014-04-28
US201462032383P 2014-08-01 2014-08-01
US201462087905P 2014-12-05 2014-12-05
US201462087914P 2014-12-05 2014-12-05
US201462087911P 2014-12-05 2014-12-05
US201462088196P 2014-12-05 2014-12-05
PCT/US2015/015128 WO2015123169A1 (fr) 2014-02-11 2015-02-10 Production de produits de polyoléfines
US15/117,363 US20160347890A1 (en) 2014-02-11 2015-02-10 Producing polyolefin products

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2015/015128 A-371-Of-International WO2015123169A1 (fr) 2014-02-11 2015-02-10 Production de produits de polyoléfines

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US18/134,800 Division US20230250204A1 (en) 2014-02-11 2023-04-14 Producing polyolefin products

Publications (1)

Publication Number Publication Date
US20160347890A1 true US20160347890A1 (en) 2016-12-01

Family

ID=52573736

Family Applications (23)

Application Number Title Priority Date Filing Date
US15/116,696 Active US9809667B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/117,789 Active US9902790B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/117,816 Active US9879106B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/118,014 Abandoned US20160362510A1 (en) 2014-02-11 2015-02-10 Method to prepare ethylene copolymers
US15/117,343 Active US10253121B2 (en) 2014-02-11 2015-02-10 Method of producing polyethylene and polyethylene thereof
US15/117,363 Abandoned US20160347890A1 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/116,250 Active US9850332B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products with improved stiffness, toughness, and processability
US15/118,307 Active US9932426B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/116,309 Active US10308742B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products with improved stiffness, toughness, and processability
US15/805,469 Active US10189923B2 (en) 2014-02-11 2017-11-07 Producing polyolefin products
US15/833,575 Active US10239977B2 (en) 2014-02-11 2017-12-06 Producing polyolefin products
US15/905,133 Active US10392456B2 (en) 2014-02-11 2018-02-26 Producing polyolefin products
US15/905,066 Active US10421829B2 (en) 2014-02-11 2018-02-26 Producing polyolefin products
US16/269,780 Active US10604606B2 (en) 2014-02-11 2019-02-07 Producing polyolefin products
US16/278,212 Active 2035-05-22 US11034783B2 (en) 2014-02-11 2019-02-18 Method of producing polyethylene and polyethylene thereof
US16/432,602 Abandoned US20190322780A1 (en) 2014-02-11 2019-06-05 Method to prepare ethylene copolymers
US16/541,767 Active 2035-08-01 US11142598B2 (en) 2014-02-11 2019-08-15 Producing polyolefin products
US17/067,287 Abandoned US20210024670A1 (en) 2014-02-11 2020-10-09 Method to prepare ethylene copolymers
US17/330,942 Active 2035-07-09 US11708438B2 (en) 2014-02-11 2021-05-26 Method of producing polyethylene and polyethylene thereof
US17/475,851 Active US11661466B2 (en) 2014-02-11 2021-09-15 Producing polyolefin products
US18/102,858 Pending US20230174694A1 (en) 2014-02-11 2023-01-30 Method to prepare ethylene copolymers
US18/134,800 Pending US20230250204A1 (en) 2014-02-11 2023-04-14 Producing polyolefin products
US18/140,165 Pending US20240076427A1 (en) 2014-02-11 2023-04-27 Producing polyolefin products

Family Applications Before (5)

Application Number Title Priority Date Filing Date
US15/116,696 Active US9809667B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/117,789 Active US9902790B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/117,816 Active US9879106B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/118,014 Abandoned US20160362510A1 (en) 2014-02-11 2015-02-10 Method to prepare ethylene copolymers
US15/117,343 Active US10253121B2 (en) 2014-02-11 2015-02-10 Method of producing polyethylene and polyethylene thereof

Family Applications After (17)

Application Number Title Priority Date Filing Date
US15/116,250 Active US9850332B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products with improved stiffness, toughness, and processability
US15/118,307 Active US9932426B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products
US15/116,309 Active US10308742B2 (en) 2014-02-11 2015-02-10 Producing polyolefin products with improved stiffness, toughness, and processability
US15/805,469 Active US10189923B2 (en) 2014-02-11 2017-11-07 Producing polyolefin products
US15/833,575 Active US10239977B2 (en) 2014-02-11 2017-12-06 Producing polyolefin products
US15/905,133 Active US10392456B2 (en) 2014-02-11 2018-02-26 Producing polyolefin products
US15/905,066 Active US10421829B2 (en) 2014-02-11 2018-02-26 Producing polyolefin products
US16/269,780 Active US10604606B2 (en) 2014-02-11 2019-02-07 Producing polyolefin products
US16/278,212 Active 2035-05-22 US11034783B2 (en) 2014-02-11 2019-02-18 Method of producing polyethylene and polyethylene thereof
US16/432,602 Abandoned US20190322780A1 (en) 2014-02-11 2019-06-05 Method to prepare ethylene copolymers
US16/541,767 Active 2035-08-01 US11142598B2 (en) 2014-02-11 2019-08-15 Producing polyolefin products
US17/067,287 Abandoned US20210024670A1 (en) 2014-02-11 2020-10-09 Method to prepare ethylene copolymers
US17/330,942 Active 2035-07-09 US11708438B2 (en) 2014-02-11 2021-05-26 Method of producing polyethylene and polyethylene thereof
US17/475,851 Active US11661466B2 (en) 2014-02-11 2021-09-15 Producing polyolefin products
US18/102,858 Pending US20230174694A1 (en) 2014-02-11 2023-01-30 Method to prepare ethylene copolymers
US18/134,800 Pending US20230250204A1 (en) 2014-02-11 2023-04-14 Producing polyolefin products
US18/140,165 Pending US20240076427A1 (en) 2014-02-11 2023-04-27 Producing polyolefin products

Country Status (16)

Country Link
US (23) US9809667B2 (fr)
EP (21) EP3998292A1 (fr)
JP (19) JP6861031B2 (fr)
KR (18) KR102496899B1 (fr)
CN (14) CN110540612B (fr)
AU (14) AU2015217402B2 (fr)
BR (9) BR112016019310B1 (fr)
CA (8) CA3155959C (fr)
ES (7) ES2918979T3 (fr)
MX (21) MX2016010312A (fr)
MY (7) MY189858A (fr)
PH (9) PH12016501557A1 (fr)
RU (12) RU2727930C1 (fr)
SA (10) SA516371655B1 (fr)
SG (20) SG11201606535YA (fr)
WO (9) WO2015123179A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11840596B2 (en) 2019-02-20 2023-12-12 Lg Chem, Ltd. Catalyst composition and method for preparing polyolefin using the same

Families Citing this family (104)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3998292A1 (fr) * 2014-02-11 2022-05-18 Univation Technologies, LLC Production de produits de polyéthylène présentant une raideur, une ténacité et une aptitude au traitement améliorées
CN106574014B (zh) * 2014-06-16 2021-04-16 尤尼威蒂恩技术有限责任公司 修改聚乙烯树脂的熔体流动比率和/或溶胀的方法
ES2928549T3 (es) * 2015-04-23 2022-11-21 Univation Tech Llc Copolímeros de polietileno que tienen una distribución de comonómero particular
FR3043687B1 (fr) * 2015-11-13 2020-07-03 Universite Blaise Pascal Clermont Ii Procede sol-gel de synthese d'un materiau luminescent de formulation generale axbyfz:mn
KR101711788B1 (ko) * 2016-03-09 2017-03-14 한화케미칼 주식회사 혼성 촉매 조성물, 이의 제조방법, 및 이를 이용하여 제조된 폴리올레핀
CN108779205B (zh) * 2016-03-31 2022-01-07 陶氏环球技术有限责任公司 烯烃聚合催化剂
WO2017184234A1 (fr) * 2016-04-22 2017-10-26 Exxonmobil Chemical Patents Inc. Feuilles de polyéthylène
US10302621B2 (en) 2016-06-15 2019-05-28 Exxonmobil Chemical Patents Inc. Methods for characterizing branching distribution in polymers
EP3293210B1 (fr) * 2016-09-12 2019-03-06 Thai Polyethylene Co., Ltd. Film polyéthylène multimodal
MY193008A (en) * 2016-09-29 2022-09-21 Dow Global Technologies Llc Multilayer stretch films having a high cling force and methods thereof
SG11201901900SA (en) * 2016-10-05 2019-04-29 Exxonmobil Chemical Patents Inc Sterically hindered metallocenes, synthesis and use
US10882932B2 (en) 2016-10-05 2021-01-05 Exxonmobil Chemical Patents Inc. Sterically hindered metallocenes, synthesis and use
WO2018084983A1 (fr) * 2016-11-03 2018-05-11 Exxonmobil Chemical Patents Inc. Système d'alimentation en catalyseur multicomposant et procédé de production de polymères
EP3538571B1 (fr) * 2016-11-08 2022-06-01 Univation Technologies, LLC Polyéthylène bimodal
WO2018106388A1 (fr) 2016-12-05 2018-06-14 Exxonmobil Chemical Patents Inc. Polyéthylènes métallocènes à large distribution orthogonale pour films
KR102212822B1 (ko) * 2016-12-05 2021-02-08 엑손모빌 케미칼 패턴츠 인코포레이티드 필름용의 브로드 오쏘고날 분포 메탈로센 폴리에틸렌
CA3046800A1 (fr) 2016-12-15 2018-06-21 Univation Technologies, Llc Evaluation de processus de polymerisation
JP2020514430A (ja) * 2016-12-19 2020-05-21 ダウ グローバル テクノロジーズ エルエルシー 伝導体外被およびその製造プロセス
WO2018147968A1 (fr) * 2017-02-13 2018-08-16 Univation Technologies, Llc Résines de polyéthylène bimodal
EP3583140B1 (fr) * 2017-02-20 2023-03-08 ExxonMobil Chemical Patents Inc. Systèmes de catalyseurs supportés et leurs procédés d'utilisation
WO2018151903A1 (fr) 2017-02-20 2018-08-23 Exxonmobil Chemical Patents Inc. Systèmes catalytiques supportés et leurs procédés d'utilisation
US10723819B2 (en) 2017-02-20 2020-07-28 Exxonmobil Chemical Patents, Inc. Supported catalyst systems and processes for use thereof
US10947329B2 (en) * 2017-05-10 2021-03-16 Univation Technologies, Llc Catalyst systems and processes for using the same
BR112019022049B1 (pt) 2017-05-17 2023-03-14 Univation Technologies, Llc Complexo de metal, complexo de metal suportado e método para formar um polímero
EP3631440B1 (fr) * 2017-06-02 2023-02-22 Univation Technologies, LLC Procédé de détermination d'une diminution relative de l'efficacité catalytique d'un catalyseur dans une solution de catalyseur
WO2018226787A1 (fr) * 2017-06-08 2018-12-13 Univation Technologies, Llc Procédé de maintien de l'indice de fluidité à chaud d'un produit polymère de polyéthylène
CN111094366B (zh) * 2017-08-04 2022-06-24 埃克森美孚化学专利公司 聚乙烯组合物和由其制备的膜
US10844150B2 (en) 2017-08-04 2020-11-24 Exxonmobil Chemical Patents Inc. Mixed catalysts with 2,6-bis(imino)pyridyl iron complexes and bridged hafnocenes
SG11202000942TA (en) 2017-08-04 2020-02-27 Exxonmobil Chemical Patents Inc Mixed catalysts with unbridged hafnocenes with -ch2-sime3 moieties
US11302459B2 (en) 2017-10-06 2022-04-12 Exxonmobil Chemical Patents Inc. Polyethylene extrudates and methods of making the same
JP6986163B2 (ja) * 2017-10-23 2021-12-22 エクソンモービル ケミカル パテンツ インコーポレイテッド 触媒系およびそれを使用する重合方法
WO2019083716A1 (fr) * 2017-10-27 2019-05-02 Univation Technologies, Llc Résines et films à base d'un copolymère de polyéthylène
US10703838B2 (en) 2017-10-31 2020-07-07 Exxonmobil Chemical Patents Inc. Mixed catalyst systems with four metallocenes on a single support
CN111587257B (zh) * 2017-10-31 2023-02-10 埃克森美孚化学专利公司 具有在单一载体上的四种茂金属的混合的催化剂体系
US10927202B2 (en) 2017-11-13 2021-02-23 Exxonmobil Chemical Patents Inc. Polyethylene compositions and articles made therefrom
WO2019094132A1 (fr) 2017-11-13 2019-05-16 Exxonmobil Chemical Patents Inc. Compositions de polyéthylène et articles fabriqués à partir de celles-ci
US11130827B2 (en) 2017-11-14 2021-09-28 Exxonmobil Chemical Patents Inc. Polyethylene compositions and articles made therefrom
WO2019099589A1 (fr) 2017-11-15 2019-05-23 Exxonmobil Chemical Patents Inc. Procédés de polymérisation
US10954328B2 (en) 2017-11-15 2021-03-23 Exxonmobil Chemical Patents Inc. Polymerization processes
CN111448226B (zh) * 2017-11-15 2023-08-25 埃克森美孚化学专利公司 聚合方法
CN111511781B (zh) * 2017-11-28 2023-07-11 埃克森美孚化学专利公司 催化剂体系和使用其的聚合方法
US10926250B2 (en) 2017-12-01 2021-02-23 Exxonmobil Chemical Patents Inc. Catalyst systems and polymerization processes for using the same
KR102405495B1 (ko) 2017-12-01 2022-06-08 엑손모빌 케미칼 패턴츠 인코포레이티드 촉매계 및 이를 사용하기 위한 중합 방법
CN108129729A (zh) * 2017-12-20 2018-06-08 宁波市鄞州智伴信息科技有限公司 一种基于永磁材料的新型可塑型磁控管的制备工艺
KR102459861B1 (ko) 2017-12-21 2022-10-27 주식회사 엘지화학 가공성이 우수한 에틸렌/1-부텐 공중합체
KR102323807B1 (ko) * 2018-01-12 2021-11-09 주식회사 엘지화학 촉매 조성물 내 브롬 화합물의 제거 방법
US10851187B2 (en) 2018-01-31 2020-12-01 Exxonmobil Chemical Patents Inc. Bridged metallocene catalysts with a pendant group 13 element, catalyst systems containing same, processes for making a polymer product using same, and products made from same
US10865258B2 (en) 2018-01-31 2020-12-15 Exxonmobil Chemical Patents Inc. Mixed catalyst systems containing bridged metallocenes with a pendant group 13 element, processes for making a polymer product using same, and products made from same
EP3752540A4 (fr) * 2018-02-12 2021-12-01 ExxonMobil Chemical Patents Inc. Systèmes et processus de catalyseur pour poly alpha-oléfine ayant une teneur élevée en vinylidène
US11459408B2 (en) * 2018-05-02 2022-10-04 Exxonmobil Chemical Patents Inc. Methods for scale-up from a pilot plant to a larger production facility
US11447587B2 (en) * 2018-05-02 2022-09-20 Exxonmobil Chemical Patents Inc. Methods for scale-up from a pilot plant to a larger production facility
WO2019246069A1 (fr) 2018-06-19 2019-12-26 Exxonmobil Chemical Patents Inc. Compositions de polyéthylène et films préparés à partir de celles-ci
US10927205B2 (en) 2018-08-30 2021-02-23 Exxonmobil Chemical Patents Inc. Polymerization processes and polymers made therefrom
US10899860B2 (en) 2018-08-30 2021-01-26 Exxonmobil Chemical Patents Inc. Polymerization processes and polymers made therefrom
WO2020046406A1 (fr) * 2018-08-30 2020-03-05 Exxonmobil Chemical Patents Inc. Procédés de polymérisation et polymères fabriqués au moyen de ces derniers
KR102258230B1 (ko) * 2018-10-19 2021-05-28 한화솔루션 주식회사 올레핀계 중합체
US20220033537A1 (en) * 2018-11-01 2022-02-03 Exxonmobil Chemical Patents Inc. On-Line Adjustment of Catalysts by Trim and Olefin Polymerization
US20210395400A1 (en) * 2018-11-01 2021-12-23 Exxonmobil Chemical Patents Inc. Mixed Catalyst Systems with Properties Tunable by Condensing Agent
WO2020092587A1 (fr) * 2018-11-01 2020-05-07 Exxonmobil Chemical Patents Inc. Ajustement en ligne d'un rapport de catalyseur mixte par polymérisation de triméthacrylate de triméthylopropane (trim) et d'oléfine avec celui-ci
CN113039212B (zh) * 2018-11-01 2023-04-14 埃克森美孚化学专利公司 干燥催化剂进料的管线内修整
EP3873948A1 (fr) * 2018-11-01 2021-09-08 ExxonMobil Chemical Patents Inc. Ajustement dans une conduite de rapport de catalyseur mixte et polymérisation d'oléfine
US20220056168A1 (en) * 2018-11-01 2022-02-24 Exxonmobil Chemical Patents Inc. Slurry Trim Feeder Modifications
CN112805289A (zh) 2018-11-06 2021-05-14 陶氏环球技术有限责任公司 烷烃可溶的非茂金属预催化剂
CA3118441A1 (fr) 2018-11-06 2020-05-14 Dow Global Technologies Llc Procede de polymerisation d'olefines utilisant un pre-catalyseur non metallocene soluble dans les alcanes
WO2020096734A1 (fr) 2018-11-06 2020-05-14 Dow Global Technologies Llc Précatalyseurs non métallocènes solubles dans des alcanes
WO2020102057A1 (fr) 2018-11-16 2020-05-22 Exxonmobil Chemical Patents Inc. Compositions de polyoléfine appropriées pour des films
KR102116476B1 (ko) * 2019-01-18 2020-05-28 대림산업 주식회사 폴리올레핀 중합 촉매 조성물, 폴리올레핀의 제조 방법 및 폴리올레핀 수지
KR102372974B1 (ko) * 2019-04-05 2022-03-10 한화솔루션 주식회사 혼성 촉매 조성물, 이를 포함하는 촉매 및 이들의 제조방법
KR20220003033A (ko) * 2019-04-30 2022-01-07 다우 글로벌 테크놀로지스 엘엘씨 금속-리간드 착물
US11014997B2 (en) 2019-05-16 2021-05-25 Chevron Phillips Chemical Company Lp Dual catalyst system for producing high density polyethylenes with long chain branching
KR102203007B1 (ko) * 2019-06-05 2021-01-14 대림산업 주식회사 다단계 연속 중합 방법을 이용한 멀티모달 폴리올레핀 제조방법
WO2021040760A1 (fr) 2019-08-28 2021-03-04 Exxonmobil Chemical Patents Inc. Compositions de polyoléfine pour des films
KR102595112B1 (ko) * 2019-09-30 2023-10-30 주식회사 엘지화학 올레핀계 중합체
KR102605409B1 (ko) * 2019-09-30 2023-11-24 주식회사 엘지화학 올레핀계 중합체
CN113795524B (zh) * 2019-09-30 2023-10-03 株式会社Lg化学 聚丙烯基复合材料
KR102547232B1 (ko) * 2019-10-24 2023-06-26 한화솔루션 주식회사 올레핀 중합용 촉매의 제조방법
KR102605269B1 (ko) * 2019-12-09 2023-11-23 한화솔루션 주식회사 기상 중합에 의한 올레핀계 중합체의 제조방법
WO2021126448A1 (fr) 2019-12-17 2021-06-24 Exxonmobil Chemical Patents Inc. Polyéthylènes à large distribution orthogonale pour films
WO2021222016A2 (fr) 2020-05-01 2021-11-04 Exxonmobil Chemical Patents Inc. Polyéthylène linéaire basse densité pour applications de film
US20230174757A1 (en) 2020-05-01 2023-06-08 Exxonmobil Chemical Patents Inc. Linear Low Density Polyethylene for Film Applications
CN115698103A (zh) * 2020-05-29 2023-02-03 陶氏环球技术有限责任公司 催化剂体系和使用其生产聚乙烯的方法
US20220403073A1 (en) * 2020-07-03 2022-12-22 Lg Chem, Ltd. Olefin-Based Polymer
CA3193394A1 (fr) 2020-09-22 2022-03-31 Bo Liu Copolymere de polyethylene bimodal et film de ce dernier
US11578156B2 (en) 2020-10-20 2023-02-14 Chevron Phillips Chemical Company Lp Dual metallocene polyethylene with improved processability for lightweight blow molded products
KR102608612B1 (ko) * 2020-11-23 2023-12-04 한화솔루션 주식회사 올레핀계 중합체 및 그 제조방법
KR102608616B1 (ko) * 2020-11-23 2023-12-04 한화솔루션 주식회사 올레핀계 중합체, 그로부터 제조된 필름 및 그 제조방법
EP4255942A1 (fr) 2020-12-02 2023-10-11 ExxonMobil Chemical Patents Inc. Compositions de polyéthylène à densité moyenne ayant une large distribution de composition orthogonale
WO2022124692A1 (fr) * 2020-12-08 2022-06-16 한화솔루션 주식회사 Polymère oléfinique, et son procédé de préparation
KR102652269B1 (ko) * 2020-12-08 2024-03-29 한화솔루션 주식회사 올레핀계 중합체 및 그 제조방법
CN116601187A (zh) * 2020-12-08 2023-08-15 韩华思路信株式会社 烯烃系聚合物、由其制造的膜及其制造方法
CA3206442A1 (fr) * 2021-02-09 2022-08-18 Rhett A. BAILLIE Metallocenes d'hafnium ayant des ligands non identiques
EP4215555A1 (fr) * 2021-03-23 2023-07-26 Lg Chem, Ltd. Polymère à base d'oléfine
WO2022210844A1 (fr) * 2021-03-31 2022-10-06 三井化学株式会社 COPOLYMER D'ÉTHYLÈNE-α-OLÈFINE, COMPOSITION DE RÉSINE THERMOPLASTIQUE ET FILM
CN113089152B (zh) * 2021-04-06 2022-11-22 军事科学院系统工程研究院军需工程技术研究所 一种原位聚合阻燃锦纶66全牵伸丝的高质高效生产方法
CN115490733A (zh) * 2021-06-17 2022-12-20 广东阿格蕾雅光电材料有限公司 含oncn四齿配体的杂环修饰的铂配合物
KR20230036257A (ko) * 2021-09-07 2023-03-14 한화솔루션 주식회사 올레핀계 중합체의 제조방법 및 이를 이용하여 제조된 올레핀계 중합체
CN117980354A (zh) 2021-10-26 2024-05-03 埃克森美孚化学专利公司 具有卓越加工性和机械性质的高度取向线性低密度聚乙烯膜
WO2023154769A1 (fr) 2022-02-11 2023-08-17 Dow Global Technologies Llc Compositions de polyéthylène à densité moyenne bimodale appropriées pour être utilisées en tant que bandes de goutte-à-goutte de micro-irrigation
WO2023215696A1 (fr) 2022-05-04 2023-11-09 Exxonmobil Chemical Patents Inc. Complexes de pyridine-2,6-bis(phénylène-phénolate) modifiés présentant une solubilité améliorée, utiles en tant que composants de catalyseur pour la polymérisation d'oléfines
WO2023215694A1 (fr) 2022-05-04 2023-11-09 Exxonmobil Chemical Patents Inc. Complexes de pyridine-2,6-bis(phénylène-phénolate) substitués présentant une solubilité améliorée, utiles en tant que composants de catalyseur pour la polymérisation d'oléfines
WO2023215693A1 (fr) 2022-05-04 2023-11-09 Exxonmobil Chemical Patents Inc. Complexes de pyridine -2,6-bis (phénylènephénolate) substitués à solubilité améliorée présentant une utilité en tant que composants de catalyseur pour la polymérisation d'oléfines
WO2023215695A1 (fr) 2022-05-04 2023-11-09 Exxonmobil Chemical Patents Inc. Complexes de pyridine-2,6-bis (phénylènephénolate) substitués présentant une solubilité accrue et utiles comme composants de catalyseurs pour la polymérisation des oléfines
WO2024030621A1 (fr) * 2022-08-05 2024-02-08 Dow Global Technologies Llc Metallocènes de zirconium symétriques comportant des ligands d'isobutyle-cyclopentadiényle
WO2024044423A1 (fr) 2022-08-22 2024-02-29 Exxonmobil Chemical Patents, Inc. Compositions de polyéthylène et films préparés à partir de celles-ci

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001009200A1 (fr) * 1999-07-29 2001-02-08 Borealis Technology Oy Ameliorations relatives a des polymeres
US20070043248A1 (en) * 2005-07-19 2007-02-22 Wu Margaret M Process to produce low viscosity poly-alpha-olefins
US20100063227A1 (en) * 2006-11-14 2010-03-11 Univation Technologies, Llc Catalyst systems and polymerization processes

Family Cites Families (130)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3067518A (en) 1958-04-02 1962-12-11 Martin A Herman Master type squaring fixture
US4003712A (en) 1970-07-29 1977-01-18 Union Carbide Corporation Fluidized bed reactor
US3709853A (en) 1971-04-29 1973-01-09 Union Carbide Corp Polymerization of ethylene using supported bis-(cyclopentadienyl)chromium(ii)catalysts
US4011382A (en) 1975-03-10 1977-03-08 Union Carbide Corporation Preparation of low and medium density ethylene polymer in fluid bed reactor
US4302566A (en) 1978-03-31 1981-11-24 Union Carbide Corporation Preparation of ethylene copolymers in fluid bed reactor
US4543399A (en) 1982-03-24 1985-09-24 Union Carbide Corporation Fluidized bed reaction systems
FR2618786B1 (fr) 1987-07-31 1989-12-01 Bp Chimie Sa Procede de polymerisation d'olefines en phase gazeuse dans un reacteur a lit fluidise
JP2857438B2 (ja) * 1988-09-30 1999-02-17 エクソン・ケミカル・パテンツ・インク 分子量分布および組成分布のせまい共重合体の線状エチレン共重合体ブレンド
US5041584A (en) 1988-12-02 1991-08-20 Texas Alkyls, Inc. Modified methylaluminoxane
TW300901B (fr) * 1991-08-26 1997-03-21 Hoechst Ag
CA2125780C (fr) * 1991-12-30 2004-07-06 Deepak R. Parikh Polymerisations d'interpolymeres d'ethylene
US5352749A (en) 1992-03-19 1994-10-04 Exxon Chemical Patents, Inc. Process for polymerizing monomers in fluidized beds
ES2128371T3 (es) * 1992-08-15 1999-05-16 Targor Gmbh Procedimiento para la obtencion de poliolefinas.
NL9201970A (nl) 1992-11-11 1994-06-01 Dsm Nv Indenylverbindingen en katalysatorcomponenten voor de polymerisatie van olefinen.
JP3365661B2 (ja) * 1992-11-19 2003-01-14 三井化学株式会社 エチレン系共重合体組成物
GB9224876D0 (en) * 1992-11-27 1993-01-13 Exxon Chemical Patents Inc Improved processing polyolefin blends
ZA943399B (en) 1993-05-20 1995-11-17 Bp Chem Int Ltd Polymerisation process
ES2141833T3 (es) * 1993-08-06 2000-04-01 Exxon Chemical Patents Inc Catalizadores de polimerizacion, su produccion y uso.
KR960704903A (ko) 1993-09-30 1996-10-09 이데미쓰 쇼스께 천이금속화합물, 올레핀중합체용 촉매, 그 촉매를 이용한 올레핀계중합체의 제조방법
AT401520B (de) * 1994-03-22 1996-09-25 Danubia Petrochem Polymere Metallocene und deren einsatz für die olefinpolymerisation
WO1995026372A1 (fr) * 1994-03-25 1995-10-05 Mobil Oil Corporation Polyethylene lineaire a faible densite
US5525678A (en) 1994-09-22 1996-06-11 Mobil Oil Corporation Process for controlling the MWD of a broad/bimodal resin produced in a single reactor
EP0743324B1 (fr) * 1995-05-16 2002-09-11 Univation Technologies LLC Production de polyéthylène utilisant des métallocènes stéréoisomériques
CN1067689C (zh) * 1995-10-20 2001-06-27 中国科学院化学研究所 一种用于合成高分子量聚乙烯的金属茂催化剂及其制备方法
US5780659A (en) * 1996-03-29 1998-07-14 Phillips Petroleum Company Substituted indenyl unbridged metallocenes
US6255426B1 (en) * 1997-04-01 2001-07-03 Exxon Chemical Patents, Inc. Easy processing linear low density polyethylene
JP2002505707A (ja) * 1997-06-14 2002-02-19 ザ ボード オブ トラスティーズ オブ ザ リーランド スタンフォード ジュニア ユニバーシティ エチレン増強高融点熱可塑性エラストマーα−オレフィン重合体合成法（ＰＲＥ／ＥＰＥ効果）
GB9712663D0 (en) * 1997-06-16 1997-08-20 Borealis As Process
FI973050A (fi) 1997-07-18 1999-01-19 Borealis As Menetelmä sellaisten olefiinipolymeerien valmistamiseksi joilla on haluttu molekyylipainojakauma
DE59807082D1 (de) 1997-07-28 2003-03-06 Basell Polyolefine Gmbh Verfahren zur herstellung von metallocenen
US20060293470A1 (en) * 2005-06-28 2006-12-28 Cao Phuong A Polymerization process using spray-dried catalyst
US6242545B1 (en) 1997-12-08 2001-06-05 Univation Technologies Polymerization catalyst systems comprising substituted hafinocenes
EP0953582A1 (fr) 1998-04-27 1999-11-03 Fina Research S.A. Production de polyoléfine
US6207606B1 (en) 1998-05-15 2001-03-27 Univation Technologies, Llc Mixed catalysts and their use in a polymerization process
EP1082355B1 (fr) 1998-05-18 2008-10-15 Chevron Phillips Chemical Company Lp Composition catalytique pour la polymerisation de monomeres
FI990003A (fi) * 1999-01-04 2000-07-05 Borealis Polymers Oy Polymeerikoostumus, menetelmä sen valmistamiseksi ja siitä valmistetut kalvot
ATE236934T1 (de) * 1999-02-22 2003-04-15 Borealis Tech Oy Olefinpolymerisationsverfahren
US6271325B1 (en) 1999-05-17 2001-08-07 Univation Technologies, Llc Method of polymerization
US6380328B1 (en) 1999-12-10 2002-04-30 Univation Technologies, Llc Catalyst systems and their use in a polymerization process
AU763705B2 (en) * 1999-10-22 2003-07-31 Univation Technologies Llc Start up methods for multiple catalyst systems
SK5482002A3 (en) 1999-10-22 2003-02-04 Univation Tech Llc Catalyst systems and their use in a polymerization process
KR100553288B1 (ko) * 1999-10-22 2006-02-22 유니베이션 테크놀로지즈, 엘엘씨 촉매 조성물, 중합 방법 및 그로부터 제조된 중합체
US6372868B1 (en) * 1999-12-07 2002-04-16 Univation Technologies, Llc Start up methods for multiple catalyst systems
US6482903B1 (en) 1999-12-15 2002-11-19 Univation Technologies, Llc Method for preparing a supported catalyst system and its use in a polymerization process
US7041617B2 (en) * 2004-01-09 2006-05-09 Chevron Phillips Chemical Company, L.P. Catalyst compositions and polyolefins for extrusion coating applications
JP2001320296A (ja) 2000-05-12 2001-11-16 Temuko Japan:Kk トランシーバ
US6608149B2 (en) 2000-12-04 2003-08-19 Univation Technologies, Llc Polymerization process
US6897273B2 (en) * 2000-12-04 2005-05-24 Univation Technologies, Llc Catalyst composition, method of polymerization and polymer therefrom
US6605675B2 (en) 2000-12-04 2003-08-12 Univation Technologies, Llc Polymerization process
CA2430197C (fr) * 2000-12-04 2008-02-12 Univation Technologies, Llc Procede de polymerisation
US20030008988A1 (en) * 2001-01-29 2003-01-09 Sasol Technology (Proprietary) Limited Polymerization
US6943227B2 (en) * 2001-06-29 2005-09-13 Japan Polypropylene Corporation Catalyst for olefin polymerization and method of polymerization of olefin
JP3660623B2 (ja) * 2001-07-05 2005-06-15 株式会社東芝 アンテナ装置
BR0211290A (pt) * 2001-07-19 2004-09-14 Univation Tech Llc Compostos de catalisador de metaloceno de baixa incorporação de comonÈmero
CN100398570C (zh) * 2001-07-19 2008-07-02 尤尼威蒂恩技术有限责任公司 含有弱共聚单体引入剂和良共聚单体引入剂的混合金属茂催化剂体系
US6936675B2 (en) * 2001-07-19 2005-08-30 Univation Technologies, Llc High tear films from hafnocene catalyzed polyethylenes
WO2004000919A1 (fr) * 2001-07-19 2003-12-31 Univation Technologies, Llc Films de polyethylene a proprietes physiques ameliorees
JP2003105029A (ja) 2001-07-25 2003-04-09 Japan Polychem Corp オレフィン重合体及びその製造方法
US6642400B2 (en) * 2001-09-26 2003-11-04 Univation Technologies, Llc Linked metallocene complexes, catalyst systems, and olefin polymerization processes using same
JP2003096124A (ja) * 2001-09-27 2003-04-03 Sumitomo Chem Co Ltd 付加重合用触媒成分、付加重合用触媒および付加重合体の製造方法、並びにメタロセン系遷移金属化合物の用途
JP2003096125A (ja) * 2001-09-27 2003-04-03 Sumitomo Chem Co Ltd 付加重合用触媒成分、付加重合用触媒および付加重合体の製造方法、並びにメタロセン系遷移金属化合物の用途
SG96700A1 (en) * 2001-09-27 2003-06-16 Sumitomo Chemical Co Catalyst component for addition polymerization, process for producing catalyst for addition polymerization and process for producing addition polymer
WO2003044061A1 (fr) * 2001-11-15 2003-05-30 Exxonmobil Chemical Patents Inc. Surveillance et commande de polymerisation a l'aide d'indicateurs avances
US6884748B2 (en) * 2002-09-04 2005-04-26 Univation Technologies, Llc Process for producing fluorinated catalysts
RU2329272C2 (ru) 2002-10-25 2008-07-20 Базелль Полиолефине Гмбх Рацемоселективное получение поддающихся выделению анса-металлоценовых бифеноксидных комплексов, имеющих относительно короткое время изомеризации
US6869903B2 (en) * 2002-11-07 2005-03-22 Univation Technologies, Llc Synthesis of polymerization catalyst components
BRPI0415341B1 (pt) 2003-10-15 2014-02-04 Método para produção de uma composição polimérica
US7119153B2 (en) * 2004-01-21 2006-10-10 Jensen Michael D Dual metallocene catalyst for producing film resins with good machine direction (MD) elmendorf tear strength
US20050182210A1 (en) 2004-02-17 2005-08-18 Natarajan Muruganandam De-foaming spray dried catalyst slurries
WO2005100414A1 (fr) * 2004-04-07 2005-10-27 Union Carbide Chemicals & Plastics Technology Corporation Methode de commande d'une polymerisation d'olefine
US7285608B2 (en) 2004-04-21 2007-10-23 Novolen Technology Holdings C.V. Metallocene ligands, metallocene compounds and metallocene catalysts, their synthesis and their use for the polymerization of olefins
EP1774485B1 (fr) * 2004-07-08 2016-05-04 ExxonMobil Chemical Patents Inc. Production de polymeres dans des conditions supercritiques
US7193017B2 (en) * 2004-08-13 2007-03-20 Univation Technologies, Llc High strength biomodal polyethylene compositions
US7432328B2 (en) * 2005-06-14 2008-10-07 Univation Technologies, Llc Enhanced ESCR bimodal HDPE for blow molding applications
GB0420396D0 (en) * 2004-09-14 2004-10-13 Bp Chem Int Ltd Polyolefins
US7064096B1 (en) 2004-12-07 2006-06-20 Nova Chemicals (International) Sa Dual catalyst on a single support
WO2007011462A1 (fr) * 2005-07-19 2007-01-25 Exxonmobil Chemical Patents Inc. Lubrifiants obtenus à partir de charges d'alpha-oléfines mélangées
US7625982B2 (en) * 2005-08-22 2009-12-01 Chevron Phillips Chemical Company Lp Multimodal polyethylene compositions and pipe made from same
US7312283B2 (en) * 2005-08-22 2007-12-25 Chevron Phillips Chemical Company Lp Polymerization catalysts and process for producing bimodal polymers in a single reactor
US7619047B2 (en) 2006-02-22 2009-11-17 Chevron Phillips Chemical Company, Lp Dual metallocene catalysts for polymerization of bimodal polymers
US8247065B2 (en) * 2006-05-31 2012-08-21 Exxonmobil Chemical Patents Inc. Linear polymers, polymer blends, and articles made therefrom
CN101472964B (zh) * 2006-06-27 2012-09-05 尤尼威蒂恩技术有限责任公司 使用茂金属催化剂的改进聚合方法、其聚合产物及最终用途
WO2008002524A2 (fr) * 2006-06-27 2008-01-03 Univation Technologies, Llc Copolymères d'éthylène et d'alpha-oléfine et procédés de polymérisation à cet effet
CA2651305A1 (fr) 2006-06-27 2008-01-03 Univation Technologies, Llc Polymeres pour produits de rotomoulage et de moulage par injection, issus de catalyseurs metallocenes
US7569784B2 (en) * 2006-10-13 2009-08-04 Eaton Corporation Electrical switching apparatus, and housing and integral pole shaft bearing assembly therefor
US7662894B2 (en) * 2006-12-19 2010-02-16 Saudi Bosic Industries Corporation Polymer supported metallocene catalyst composition for polymerizing olefins
TWI404730B (zh) * 2007-02-05 2013-08-11 Univation Tech Llc 控制聚合物性質之方法
WO2008105546A1 (fr) * 2007-02-26 2008-09-04 Sumitomo Chemical Company, Limited Procédé de production de polymère oléfinique
CN101679540B (zh) * 2007-05-02 2012-09-05 Lg化学株式会社 聚烯烃及其制备方法
TW200932762A (en) * 2007-10-22 2009-08-01 Univation Tech Llc Polyethylene compositions having improved properties
TW200936619A (en) * 2007-11-15 2009-09-01 Univation Tech Llc Polymerization catalysts, methods of making, methods of using, and polyolefin products made therefrom
RU2476446C2 (ru) * 2007-11-20 2013-02-27 Юнивейшн Текнолоджиз, Ллк Способ получения полиолефинов
JP5311805B2 (ja) 2007-11-21 2013-10-09 日本ポリエチレン株式会社 オレフィン重合用触媒及びそれを用いたオレフィンの重合方法
CN101939343B (zh) * 2007-12-18 2013-10-02 尤尼威蒂恩技术有限责任公司 聚合期间控制双峰催化剂活性的方法
US8436114B2 (en) * 2010-10-21 2013-05-07 Exxonmobil Chemical Patents Inc. Polyethylene and process for production thereof
CA2711162A1 (fr) 2007-12-31 2009-07-16 Dow Global Technologies Inc. Procede de polymerisation de polymeres a base d'olefines
US7884163B2 (en) 2008-03-20 2011-02-08 Chevron Phillips Chemical Company Lp Silica-coated alumina activator-supports for metallocene catalyst compositions
US20090240010A1 (en) 2008-03-20 2009-09-24 Mcdaniel Max P Alumina-silica activator-supports for metallocene catalyst compositions
CN102015782B (zh) * 2008-04-28 2012-10-03 尤尼威蒂恩技术有限责任公司 制备催化剂体系的方法
US8372930B2 (en) * 2008-06-20 2013-02-12 Exxonmobil Chemical Patents Inc. High vinyl terminated propylene based oligomers
ES2420117T3 (es) 2008-06-20 2013-08-22 Exxonmobil Chemical Patents Inc. Oligómeros basados en propileno terminado en vinilo superior
US8580902B2 (en) * 2008-08-01 2013-11-12 Exxonmobil Chemical Patents Inc. Catalyst system, process for olefin polymerization, and polymer compositions produced therefrom
US8846188B2 (en) * 2008-09-25 2014-09-30 Basell Poliolefine GmbH Impact resistant LLDPE composition and films made thereof
US8664140B2 (en) 2008-12-17 2014-03-04 Basell Polyolefine Gmbh Catalyst system for olefin polymerization, its production and use
EP2430053A1 (fr) * 2009-05-14 2012-03-21 Univation Technologies, LLC Systèmes catalytiques métalliques mixtes ayant une réponse sur mesure à l'hydrogène
BR122013014965B1 (pt) 2009-06-16 2019-10-29 Chevron Phillps Chemical Company Lp composições compreendendo polialfaolefina e composições compreendendo produto oligomérico alfa olefina
US8957167B2 (en) 2009-07-28 2015-02-17 Univation Technologies, Llc Polymerization process using a supported constrained geometry catalyst
WO2011072851A1 (fr) 2009-12-18 2011-06-23 Basell Polyolefine Gmbh Procédé de préparation de catalyseurs supportés
WO2011090861A1 (fr) * 2010-01-22 2011-07-28 Exxonmobil Chemical Patents Inc. Compositions d'huile lubrifiante et procédé pour préparer celles-ci
WO2011103402A1 (fr) * 2010-02-22 2011-08-25 Univation Technologies, Llc Systèmes catalyseurs et procédés d'utilisation de ces derniers pour produire des produits de polyoléfine
US8999875B2 (en) 2010-05-28 2015-04-07 Basell Polyolefine Gmbh Process for preparing a supported catalyst system for olefin polymerization, the catalyst system and its use
US8288487B2 (en) * 2010-07-06 2012-10-16 Chevron Phillips Chemical Company Lp Catalysts for producing broad molecular weight distribution polyolefins in the absence of added hydrogen
US8932975B2 (en) 2010-09-07 2015-01-13 Chevron Phillips Chemical Company Lp Catalyst systems and methods of making and using same
CA2734167C (fr) * 2011-03-15 2018-03-27 Nova Chemicals Corporation Film de polyethylene
JP2013053308A (ja) * 2011-08-11 2013-03-21 Sumitomo Chemical Co Ltd オレフィン重合体の製造方法、エチレン系重合体および成形体
WO2013028283A1 (fr) * 2011-08-19 2013-02-28 Univation Technologies, Llc Systèmes de catalyseur et leurs procédés d'utilisation pour la production de produits de polyoléfine
CN102382217B (zh) * 2011-08-30 2013-05-08 浙江大学 分子量可调的双峰或宽峰分布聚乙烯的制备方法
JP5960831B2 (ja) * 2011-09-23 2016-08-02 エクソンモービル ケミカル パテンツ インコーポレイテッド 改質ポリエチレン組成物
ES2729280T3 (es) * 2011-11-08 2019-10-31 Univation Tech Llc Métodos para producir poliolefinas con sistemas catalíticos
US9115233B2 (en) 2012-06-21 2015-08-25 Nova Chemicals (International) S.A. Ethylene copolymer compositions, film and polymerization processes
CA2780508A1 (fr) * 2012-06-21 2013-12-21 Nova Chemicals Corporation Composition de polyethylene, pellicule et procede de polymerisation
CA2798855C (fr) * 2012-06-21 2021-01-26 Nova Chemicals Corporation Copolymere d'ethylene ayant une incorporation de comonomere inverse
ES2606684T3 (es) * 2012-11-07 2017-03-27 Chevron Phillips Chemical Company Lp Resinas de poliolefina de baja densidad y películas preparadas a partir de éstas
DK2931763T3 (en) * 2012-12-14 2018-04-16 Nova Chem Int Sa ETHYLENE COPOLYMER COMPOSITIONS, MOVIES AND POLYMERIZATION PROCEDURES
WO2014099307A1 (fr) * 2012-12-21 2014-06-26 Exxonmobil Chemical Patents Inc. Polyéthylène ramifié par un traitement amélioré et films hautement résistants à la déchirure fabriqués à partir de ceux-ci
KR102113899B1 (ko) * 2013-02-07 2020-05-21 유니베이션 테크놀로지즈, 엘엘씨 폴리올레핀의 제조
EP2970525B1 (fr) * 2013-03-15 2021-03-24 Univation Technologies, LLC Système de catalyseur multiple comprenant des métallocènes et des complexes de ligand à base d'azote tridentate pour la polymérisation des oléfines
US9156970B2 (en) * 2013-09-05 2015-10-13 Chevron Phillips Chemical Company Lp Higher density polyolefins with improved stress crack resistance
US9181370B2 (en) * 2013-11-06 2015-11-10 Chevron Phillips Chemical Company Lp Low density polyolefin resins with low molecular weight and high molecular weight components, and films made therefrom
EP3998292A1 (fr) * 2014-02-11 2022-05-18 Univation Technologies, LLC Production de produits de polyéthylène présentant une raideur, une ténacité et une aptitude au traitement améliorées

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001009200A1 (fr) * 1999-07-29 2001-02-08 Borealis Technology Oy Ameliorations relatives a des polymeres
US20070043248A1 (en) * 2005-07-19 2007-02-22 Wu Margaret M Process to produce low viscosity poly-alpha-olefins
US20100063227A1 (en) * 2006-11-14 2010-03-11 Univation Technologies, Llc Catalyst systems and polymerization processes

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Reybuck et al claims 17 , 21 , 23 , 25-27 , 32 , 34 , 37 , 40-41 and 43 co-pending application 15/118 , 014 *
Reybuck et al. Journal of Polymer Science, Part A: Polymer Chemistry, 42(13), 3323-3331, 2004 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11840596B2 (en) 2019-02-20 2023-12-12 Lg Chem, Ltd. Catalyst composition and method for preparing polyolefin using the same

Also Published As

Publication number Publication date
MY189929A (en) 2022-03-22
AU2015217387B2 (en) 2018-12-06
JP2020143296A (ja) 2020-09-10
CN114805656B (zh) 2024-02-27
KR102378586B1 (ko) 2022-03-25
US20180186912A1 (en) 2018-07-05
KR20160119817A (ko) 2016-10-14
US11142598B2 (en) 2021-10-12
BR112016019327B1 (pt) 2021-09-21
RU2016136093A3 (fr) 2018-09-28
EP4317200A3 (fr) 2024-05-15
AU2015217387A1 (en) 2016-09-15
SG10201706683TA (en) 2017-09-28
MY181775A (en) 2021-01-06
CN105980424A (zh) 2016-09-28
EP3105266B1 (fr) 2020-03-25
KR102394133B1 (ko) 2022-05-09
US10421829B2 (en) 2019-09-24
US20210284770A1 (en) 2021-09-16
JP2021036050A (ja) 2021-03-04
AU2015217402B2 (en) 2018-11-08
CN110330581B (zh) 2022-06-28
BR112016018423B1 (pt) 2021-06-22
BR112016019310B1 (pt) 2022-08-02
AU2018282274A1 (en) 2019-01-17
RU2697832C1 (ru) 2019-08-21
BR112016018402B1 (pt) 2021-06-15
MX2022002890A (es) 2022-04-06
KR20210135629A (ko) 2021-11-15
AU2015217388A1 (en) 2016-09-15
MX2022005281A (es) 2022-05-24
MY193760A (en) 2022-10-27
JP6527165B2 (ja) 2019-06-05
CN105980423B (zh) 2022-03-25
JP2019163476A (ja) 2019-09-26
SG11201606539RA (en) 2016-09-29
BR112016019314B1 (pt) 2021-11-03
MX2022005712A (es) 2022-06-08
KR102362123B1 (ko) 2022-02-14
CN110330581A (zh) 2019-10-15
EP3660058A1 (fr) 2020-06-03
EP3105262A1 (fr) 2016-12-21
CA2938843A1 (fr) 2015-08-20
MX2022006494A (es) 2022-07-04
SA516371656B1 (ar) 2020-02-02
MX2016010381A (es) 2016-11-30
US20170008983A1 (en) 2017-01-12
US20160362510A1 (en) 2016-12-15
RU2016135542A (ru) 2018-03-02
SA516371659B1 (ar) 2018-09-06
CA2938740C (fr) 2022-06-21
KR20160124788A (ko) 2016-10-28
KR102354757B1 (ko) 2022-02-08
PH12016501561A1 (en) 2016-09-14
CN106029711B (zh) 2019-05-10
PH12016501558A1 (en) 2016-09-14
BR112016019329B1 (pt) 2021-09-28
MX2022002888A (es) 2022-04-06
RU2016136183A3 (fr) 2018-09-28
RU2693828C2 (ru) 2019-07-05
PH12016501556A1 (en) 2016-09-14
RU2016136092A3 (fr) 2018-08-31
CN105980424B (zh) 2019-05-21
SG11201606532QA (en) 2016-09-29
WO2015123171A3 (fr) 2015-10-22
KR20160122178A (ko) 2016-10-21
PH12016501560A1 (en) 2016-09-14
BR112016018402A2 (pt) 2017-08-08
SA516371661B1 (ar) 2020-11-03
SA516371654B1 (ar) 2022-08-14
KR20210148433A (ko) 2021-12-07
CN109535299B (zh) 2022-06-28
US20170183433A1 (en) 2017-06-29
PH12016501557A1 (en) 2016-09-14
US20190177452A1 (en) 2019-06-13
WO2015123164A1 (fr) 2015-08-20
CN106034402B (zh) 2019-05-31
BR112016019324B1 (pt) 2021-11-09
CA3155959C (fr) 2024-02-06
EP3805278A1 (fr) 2021-04-14
RU2016136092A (ru) 2018-03-15
MX2022003089A (es) 2022-04-11
SG11201606592VA (en) 2016-09-29
CN105992775B (zh) 2019-10-25
US11034783B2 (en) 2021-06-15
EP3943514A1 (fr) 2022-01-26
CA2938846A1 (fr) 2015-08-20
AU2015217400B2 (en) 2018-12-20
CN105992775A (zh) 2016-10-05
US20180066088A1 (en) 2018-03-08
KR20160121541A (ko) 2016-10-19
AU2015217394A1 (en) 2016-09-15
RU2670755C9 (ru) 2018-12-17
WO2015123172A1 (fr) 2015-08-20
RU2016136183A (ru) 2018-03-15
PH12016501559A1 (en) 2016-09-14
US20220002455A1 (en) 2022-01-06
EP4317200A2 (fr) 2024-02-07
AU2015217394B2 (en) 2018-12-13
JP2017505372A (ja) 2017-02-16
EP3105257B1 (fr) 2020-10-21
RU2018141057A (ru) 2019-03-21
CN106029710B (zh) 2019-08-30
CA3206038A1 (fr) 2015-08-20
US11708438B2 (en) 2023-07-25
AU2020273299B2 (en) 2022-09-29
MX2022008903A (es) 2022-08-16
BR112016018423A2 (pt) 2017-08-08
US10308742B2 (en) 2019-06-04
CN105992776A (zh) 2016-10-05
KR20220043228A (ko) 2022-04-05
US20170022309A1 (en) 2017-01-26
US10239977B2 (en) 2019-03-26
KR102403962B1 (ko) 2022-06-02
RU2689991C1 (ru) 2019-05-30
US20210024670A1 (en) 2021-01-28
JP2017505846A (ja) 2017-02-23
EP3105259A2 (fr) 2016-12-21
WO2015123165A3 (fr) 2015-10-08
US20160347874A1 (en) 2016-12-01
WO2015123179A1 (fr) 2015-08-20
BR112016019334B1 (pt) 2021-03-09
KR20160121543A (ko) 2016-10-19
KR20210158429A (ko) 2021-12-30
JP2021073361A (ja) 2021-05-13
US20230174694A1 (en) 2023-06-08
KR102324441B1 (ko) 2021-11-11
JP2017505371A (ja) 2017-02-16
BR112016019327A2 (pt) 2017-08-15
JP6538703B2 (ja) 2019-07-03
US10189923B2 (en) 2019-01-29
AU2018282375B2 (en) 2020-09-03
AU2015217388B2 (en) 2018-09-20
AU2015217390B2 (en) 2018-11-29
MY186379A (en) 2021-07-21
KR102329464B1 (ko) 2021-11-23
EP3105258A1 (fr) 2016-12-21
CN109535299A (zh) 2019-03-29
PH12016501559B1 (en) 2016-09-14
PH12016501563A1 (en) 2017-02-06
KR102514764B1 (ko) 2023-03-29
US9879106B2 (en) 2018-01-30
SG10201709279RA (en) 2017-12-28
WO2015123169A1 (fr) 2015-08-20
CA2938841A1 (fr) 2015-08-20
RU2016135513A3 (fr) 2018-08-31
CN106029712A (zh) 2016-10-12
CA2938740A1 (fr) 2015-08-20
CA2938836A1 (fr) 2015-08-20
CA2938839A1 (fr) 2015-08-20
US20160347886A1 (en) 2016-12-01
EP3105265B1 (fr) 2021-06-02
EP3105257A2 (fr) 2016-12-21
US20180186911A1 (en) 2018-07-05
BR112016019310A2 (pt) 2018-05-08
KR20210137229A (ko) 2021-11-17
CN105980423A (zh) 2016-09-28
CA2938843C (fr) 2022-11-15
JP2019143160A (ja) 2019-08-29
CN106034402A (zh) 2016-10-19
CN106062016A (zh) 2016-10-26
MY192954A (en) 2022-09-19
JP2017505374A (ja) 2017-02-16
CN106029712B (zh) 2019-05-21
JP2021102776A (ja) 2021-07-15
SG11201606537VA (en) 2016-09-29
ES2944883T3 (es) 2023-06-26
JP6532881B2 (ja) 2019-06-19
CN106062016B (zh) 2019-10-08
KR20160119801A (ko) 2016-10-14
JP2020055811A (ja) 2020-04-09
AU2018282274B2 (en) 2020-08-06
JP7108065B2 (ja) 2022-07-27
PH12016501555A1 (en) 2016-09-14
AU2019200925A1 (en) 2019-02-28
MX2016010384A (es) 2017-01-05
SA516371657B1 (ar) 2019-10-30
MX2022002889A (es) 2022-04-06
AU2015217393B2 (en) 2018-12-20
MX2016010307A (es) 2016-12-20
SG10201800002WA (en) 2018-02-27
AU2015217400A1 (en) 2016-09-15
MX2016010387A (es) 2017-02-28
KR20160121540A (ko) 2016-10-19
CA2938836C (fr) 2023-05-02
MY196468A (en) 2023-04-12
AU2020204208A1 (en) 2020-07-16
ES2959613T3 (es) 2024-02-27
KR20160123320A (ko) 2016-10-25
AU2015217402A1 (en) 2016-09-15
AU2015217402A8 (en) 2018-11-29
SG10201800009QA (en) 2018-02-27
WO2015123168A8 (fr) 2016-06-02
RU2674254C1 (ru) 2018-12-06
US9809667B2 (en) 2017-11-07
SG11201606535YA (en) 2016-09-29
EP3663323A1 (fr) 2020-06-10
KR20160121542A (ko) 2016-10-19
SG11201606534UA (en) 2016-09-29
JP7222006B2 (ja) 2023-02-14
KR20210106026A (ko) 2021-08-27
JP2017506281A (ja) 2017-03-02
WO2015123171A2 (fr) 2015-08-20
CA3155959A1 (fr) 2015-08-20
KR102496899B1 (ko) 2023-02-07
US10253121B2 (en) 2019-04-09
KR102362120B1 (ko) 2022-02-14
US20240076427A1 (en) 2024-03-07
KR102454826B1 (ko) 2022-10-17
EP3105262B1 (fr) 2022-03-30
KR20210129251A (ko) 2021-10-27
SA516371658B1 (ar) 2019-12-10
JP2021073360A (ja) 2021-05-13
RU2016135513A (ru) 2018-03-06
AU2019200925B2 (en) 2020-04-02
CN110330582B (zh) 2022-04-12
KR102344094B1 (ko) 2021-12-30
CA2938839C (fr) 2023-09-19
MX2016010312A (es) 2016-12-20
SG10201800007UA (en) 2018-02-27
EP3105263A1 (fr) 2016-12-21
EP3105263B1 (fr) 2023-04-05
EP3998292A1 (fr) 2022-05-18
BR112016018400B1 (pt) 2021-06-08
MY189858A (en) 2022-03-14
CN114805656A (zh) 2022-07-29
JP7229846B2 (ja) 2023-02-28
EP3816196A2 (fr) 2021-05-05
MX2016010310A (es) 2016-12-20
MX2022005282A (es) 2022-05-24
US20190169333A1 (en) 2019-06-06
AU2015217386A1 (en) 2016-09-08
WO2015123168A1 (fr) 2015-08-20
WO2015123177A1 (fr) 2015-08-20
JP6861031B2 (ja) 2021-04-21
MX2022005710A (es) 2022-06-08
JP7208176B2 (ja) 2023-01-18
ES2918979T3 (es) 2022-07-21
JP7212445B2 (ja) 2023-01-25
WO2015123166A1 (fr) 2015-08-20
EP4198064A1 (fr) 2023-06-21
ES2931331T3 (es) 2022-12-28
JP6613240B2 (ja) 2019-11-27
AU2015217390A1 (en) 2016-09-15
RU2016136093A (ru) 2018-03-15
EP3677605A1 (fr) 2020-07-08
US11661466B2 (en) 2023-05-30
EP3105261B1 (fr) 2022-10-12
BR112016018400A2 (pt) 2017-08-08
CN105992776B (zh) 2019-05-21
JP2017505376A (ja) 2017-02-16
SA516371652B1 (ar) 2019-06-13
AU2015217391B2 (en) 2018-11-15
EP3105265A1 (fr) 2016-12-21
SG10201710927RA (en) 2018-02-27
EP3105266A1 (fr) 2016-12-21
CN110540612A (zh) 2019-12-06
EP3998293A1 (fr) 2022-05-18
SG10201800006YA (en) 2018-02-27
JP6970240B2 (ja) 2021-11-24
WO2015123165A2 (fr) 2015-08-20
BR112016019334A2 (pt) 2018-05-08
SG10201709280WA (en) 2018-01-30
RU2691994C2 (ru) 2019-06-19
BR112016019324A2 (pt) 2018-05-08
US9850332B2 (en) 2017-12-26
MX2016010309A (es) 2016-12-20
AU2015217391A1 (en) 2016-09-15
JP6836903B2 (ja) 2021-03-03
CA2938841C (fr) 2023-10-24
US10392456B2 (en) 2019-08-27
SG11201606571QA (en) 2016-09-29
MX2022005711A (es) 2022-06-08
KR102323279B1 (ko) 2021-11-08
MX2016010394A (es) 2016-12-14
JP6970161B2 (ja) 2021-11-24
EP3105258B1 (fr) 2024-03-06
JP2017505370A (ja) 2017-02-16
SG10201800008XA (en) 2018-02-27
ES2836145T3 (es) 2021-06-24
RU2767902C1 (ru) 2022-03-22
PH12016501562A1 (en) 2017-02-06
RU2725653C1 (ru) 2020-07-03
RU2734065C2 (ru) 2020-10-12
KR102329477B1 (ko) 2021-11-24
US9902790B2 (en) 2018-02-27
RU2018141057A3 (fr) 2019-09-03
US20160347888A1 (en) 2016-12-01
EP3816196A3 (fr) 2021-07-14
CN106029711A (zh) 2016-10-12
AU2015217393A1 (en) 2016-09-15
JP6833902B2 (ja) 2021-02-24
US20180105625A1 (en) 2018-04-19
MX2022005279A (es) 2022-05-24
KR20210054044A (ko) 2021-05-12
AU2018282375A1 (en) 2019-01-17
CN110540612B (zh) 2022-08-12
JP2017508834A (ja) 2017-03-30
EP3105264B1 (fr) 2023-09-06
RU2016135542A3 (fr) 2018-09-28
AU2020273299A1 (en) 2020-12-17
JP6709160B2 (ja) 2020-06-10
CN110330582A (zh) 2019-10-15
ES2786323T3 (es) 2020-10-09
US10604606B2 (en) 2020-03-31
JP2017507017A (ja) 2017-03-16
KR20220000908A (ko) 2022-01-04
EP3105264A1 (fr) 2016-12-21
SG10201701980PA (en) 2017-05-30
SG11201606575TA (en) 2016-09-29
US20190322780A1 (en) 2019-10-24
US9932426B2 (en) 2018-04-03
AU2015217386B2 (en) 2018-12-06
US20190367650A1 (en) 2019-12-05
CN106029710A (zh) 2016-10-12
KR102321784B1 (ko) 2021-11-05
KR102440033B1 (ko) 2022-09-06
JP2021073362A (ja) 2021-05-13
JP7277501B2 (ja) 2023-05-19
MX2016010378A (es) 2016-11-30
SA516371655B1 (ar) 2020-08-31
SG11201606564YA (en) 2016-09-29
RU2734065C9 (ru) 2020-11-26
EP3663323B1 (fr) 2024-03-20
EP3105259B1 (fr) 2020-11-11
BR112016019329A2 (pt) 2018-05-08
RU2670986C2 (ru) 2018-10-29
US20230250204A1 (en) 2023-08-10
EP3819314A2 (fr) 2021-05-12
CA2938846C (fr) 2022-07-12
SA516371653B1 (ar) 2019-10-09
RU2670755C2 (ru) 2018-10-25
KR102293490B1 (ko) 2021-08-26
RU2727930C1 (ru) 2020-07-27
SA519401457B1 (ar) 2021-03-16
KR102454827B1 (ko) 2022-10-17
JP6526030B2 (ja) 2019-06-05
EP3105261A1 (fr) 2016-12-21
EP3778671A1 (fr) 2021-02-17
ES2858098T3 (es) 2021-09-29
JP2020090678A (ja) 2020-06-11
US20160347889A1 (en) 2016-12-01
BR112016019314A2 (pt) 2017-08-15
SG10201710935UA (en) 2018-02-27
WO2015123171A8 (fr) 2016-09-01
AU2015217391B9 (en) 2018-12-13
EP3819314A3 (fr) 2021-07-21

Similar Documents

Publication Publication Date Title
US11661466B2 (en) Producing polyolefin products

Legal Events

Date Code Title Description
STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STCV Information on status: appeal procedure

Free format text: NOTICE OF APPEAL FILED

STCV Information on status: appeal procedure

Free format text: APPEAL BRIEF (OR SUPPLEMENTAL BRIEF) ENTERED AND FORWARDED TO EXAMINER

STCV Information on status: appeal procedure

Free format text: EXAMINER'S ANSWER TO APPEAL BRIEF MAILED

STCV Information on status: appeal procedure

Free format text: ON APPEAL -- AWAITING DECISION BY THE BOARD OF APPEALS

STCV Information on status: appeal procedure

Free format text: BOARD OF APPEALS DECISION RENDERED

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STCV Information on status: appeal procedure

Free format text: NOTICE OF APPEAL FILED

STCV Information on status: appeal procedure

Free format text: APPEAL BRIEF (OR SUPPLEMENTAL BRIEF) ENTERED AND FORWARDED TO EXAMINER

STCV Information on status: appeal procedure

Free format text: EXAMINER'S ANSWER TO APPEAL BRIEF MAILED

STCV Information on status: appeal procedure

Free format text: ON APPEAL -- AWAITING DECISION BY THE BOARD OF APPEALS

STCB Information on status: application discontinuation

Free format text: ABANDONED -- AFTER EXAMINER'S ANSWER OR BOARD OF APPEALS DECISION