WO2022089423A1 - 用于制备烯烃聚合催化剂的固体组分及其制备方法和应用 - Google Patents

用于制备烯烃聚合催化剂的固体组分及其制备方法和应用 Download PDF

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WO2022089423A1
WO2022089423A1 PCT/CN2021/126397 CN2021126397W WO2022089423A1 WO 2022089423 A1 WO2022089423 A1 WO 2022089423A1 CN 2021126397 W CN2021126397 W CN 2021126397W WO 2022089423 A1 WO2022089423 A1 WO 2022089423A1
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general formula
chain
straight
hydrogen
branched alkyl
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PCT/CN2021/126397
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English (en)
French (fr)
Inventor
李威莅
夏先知
周俊领
刘月祥
凌永泰
刘涛
赵瑾
高富堂
任春红
谭扬
陈龙
Original Assignee
中国石油化工股份有限公司
中国石油化工股份有限公司北京化工研究院
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Priority claimed from CN202011157579.4A external-priority patent/CN114478857B/zh
Priority claimed from CN202011156589.6A external-priority patent/CN114478853B/zh
Priority claimed from CN202011157626.5A external-priority patent/CN114478859B/zh
Priority claimed from CN202011157613.8A external-priority patent/CN114478858B/zh
Application filed by 中国石油化工股份有限公司, 中国石油化工股份有限公司北京化工研究院 filed Critical 中国石油化工股份有限公司
Priority to JP2023525540A priority Critical patent/JP2023546624A/ja
Priority to EP21885150.9A priority patent/EP4234590A1/en
Priority to US18/250,551 priority patent/US20230416424A1/en
Priority to KR1020237017908A priority patent/KR20230097111A/ko
Publication of WO2022089423A1 publication Critical patent/WO2022089423A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/02—Carriers therefor
    • 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
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/04—Monomers containing three or four carbon atoms
    • C08F110/06—Propene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • 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
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/04—Monomers containing three or four carbon atoms
    • C08F10/06—Propene
    • 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
    • C08F4/642—Component covered by group C08F4/64 with an organo-aluminium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/51—Spheres

Definitions

  • the present invention relates to a solid component (also called a carrier) for preparing an olefin polymerization catalyst, a preparation method thereof, and an application in the preparation of an olefin polymerization catalyst.
  • a solid component also called a carrier
  • Most of the catalysts used for olefin polymerization are prepared by supporting titanium halide on active anhydrous magnesium chloride.
  • one method used to prepare activated magnesium chloride is to react anhydrous ⁇ - MgCl2 with an alcohol to form an adduct, and then use this adduct as a carrier to support titanium halide to prepare a solid set of olefin polymerization catalysts point.
  • the magnesium chloride alcoholate can be prepared by methods such as spray drying, spray cooling, high pressure extrusion, high speed stirring, emulsifier, supergravity rotating bed and the like.
  • the Lewis base compounds can be ethers, esters and compounds of the formula RX m , wherein R is an alkyl group of carbon atoms of 1-20, and X has the structure of -NH 2 , -NHR or -OH.
  • Activated magnesium chloride supports can also be prepared by using magnesium alkoxides as raw materials.
  • CN1016422B discloses a method for preparing a ZN catalyst solid component, which is prepared by reacting soluble dialkylmagnesium with a transition metal halide in the presence of transition metal alkoxide, and then precipitating the solid component with liquid hydrocarbon.
  • the alkoxy group in the magnesium dialkoxide used is a linear alkoxy group containing 6 to 12 carbon atoms or a branched alkoxy group of 5 to 12 carbon atoms, so as to form a magnesium alkoxide soluble in liquid hydrocarbons solution, however such magnesium alkoxides are difficult to obtain.
  • CN1177868C discloses a preparation method for olefin polymerization catalyst precursor, which is prepared by reacting magnesium alkoxide and titanium alkoxide in the presence of a blocking agent to form a solid complex.
  • the magnesium alkoxide is diethoxide magnesium
  • the titanium alkoxide is tetraethoxide titanium.
  • CN101056894A discloses a catalyst for propylene polymerization, which is prepared by reacting dialkoxymagnesium with a titanium halide compound or a halogenated silane compound and an internal electron donor in the presence of an organic solvent.
  • the general formula of magnesium dialkoxide is Mg(OR) 2 , wherein R is a C1-C6 alkyl group, and it is prepared by the reaction of magnesium metal and alcohol.
  • CN101190953A discloses a method for preparing a solid component of an olefin polymerization catalyst, which comprises mixing a magnesium-containing complex with the general formula ClMg(OR) ⁇ n(ROH) with an electron donor compound and a titanium tetrahalide in the presence of an inert hydrocarbon, respectively. reaction prepared.
  • the magnesium-containing complex is prepared by reacting metal magnesium powder with alcohol, wherein R in the general formula is a C1-C5 alkyl group, and n is 0.1-1.0.
  • Patent application CN200910235565 discloses a compound that can be used as an olefin polymerization catalyst carrier and a preparation method thereof. The method heats magnesium halide, an alcohol compound and an inert dispersion medium to form a magnesium halide alcohol compound solution, and then mixes the solution with epoxy resin. Ethane compounds react to form spherical carriers.
  • Patent application CN2013104913936 teaches adding a polymer dispersion stabilizer in the preparation process of the above-mentioned carrier, so that solid particles with good particle shape and narrow particle size distribution can be obtained without adding an inert dispersion medium, thereby improving the single-pot yield, Reduced solvent recovery costs.
  • patent applications CN111072804A, CN111072811A, CN107915792A, CN107915793A, CN107915795A, CN109400763A, CN109400778A, CN111072803A have successively disclosed adding zinc halide, alkali metal halide, manganese halide, halide metal such as halides to improve the particle morphology and polymerization properties of the carrier.
  • An object of the present invention is to provide a solid component for the preparation of an olefin polymerization catalyst, which can be used as a support for the preparation of an olefin polymerization catalyst, especially a propylene polymerization or copolymerization catalyst.
  • the solid components/carriers of the present invention exhibit good particle morphology, eg, without the problems of sticking between carrier particles encountered in the prior art.
  • the catalyst prepared with the solid component as a carrier shows higher polymerization activity and stereospecificity and/or good hydrogen modulation sensitivity when used for olefin polymerization, especially propylene polymerization or copolymerization.
  • Another object of the present invention is to provide a method for preparing a solid component for preparing an olefin polymerization catalyst.
  • the method of the invention has simple preparation process and low energy consumption in the preparation process.
  • Yet another object of the present invention is to provide an olefin polymerization catalyst component comprising the reaction product of the support/solid component of the present invention with a titanium compound and an internal electron donor compound.
  • Yet another object of the present invention is to provide an olefin polymerization catalyst system.
  • Yet another object of the present invention is to provide a process for the polymerization of olefins.
  • FIG. 1A is an optical microscope photo of the morphology of the solid component particles prepared in Example 1 (magnification 160 times).
  • FIG. 1B is an optical microscope photograph of the morphology of the solid component particles prepared in Example 1 (400 times magnification).
  • FIG. 2 is an optical microscope photograph of the morphology of the solid component particles prepared in Example 4 (magnification 160 times).
  • 3A is a topographical optical microscope photograph of the solid component prepared in Comparative Example 1 (magnification 160 times).
  • FIG. 3B is an optical microscope photograph of the morphology of the solid component prepared in Comparative Example 1 (magnification 400 times).
  • FIG. 4 is an optical microscope photograph of the morphology of the solid catalyst component particles prepared in Example 1.
  • FIG. 4 is an optical microscope photograph of the morphology of the solid catalyst component particles prepared in Example 1.
  • FIG. 5 is a topographical optical microscope photograph of the catalyst component prepared in Comparative Example 1.
  • FIG. 5 is a topographical optical microscope photograph of the catalyst component prepared in Comparative Example 1.
  • Figure 6A is an optical microscope photo of the morphology of the carrier particles prepared in Example 14, with a magnification of 160.
  • 6B is an electron microscope photograph of the carrier particles prepared in Example 14.
  • FIG. 7 is a topographical optical microscope photograph of the catalyst component prepared in Example 24.
  • FIG. 7 is a topographical optical microscope photograph of the catalyst component prepared in Example 24.
  • 8A is an optical microscope photo of the morphology of the carrier particles prepared in Example 27, with a magnification of 160.
  • 8B is an optical microscope photo of the morphology of the carrier particles prepared in Example 27, with a magnification of 400.
  • 8C is an electron microscope photograph of the carrier particles prepared in Example 27.
  • the present invention provides a solid component for preparing an olefin polymerization catalyst, comprising:
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted C 1 -C 5 straight-chain or branched chain Alkyl;
  • X is halogen;
  • m is 0.1-1.9;
  • n is 0.1-1.9;
  • m+n 2;
  • other metal components other than magnesium preferably the other metal components are one or both of iron and copper; preferably the other metal components are in the solid component
  • the weight percentage in the metal is 0-1%
  • R 5 and R 7 are the same or different, and are hydrogen or unsubstituted or hydroxy-substituted C 1 -C 8 linear or branched alkyl; R 6 is C 1 -C 8 linear or branched chain alkylene; or
  • the Lewis base is an amide compound represented by the general formula (II'),
  • R 10 is hydrogen, amino or C 1 -C 8 linear or branched alkyl
  • R 11 and R 12 are the same or different, and are hydrogen or C 1 -C 8 linear or branched alkyl .
  • solid component for preparing olefin polymerization catalyst and “support (or simply “support”) for preparing olefin polymerization catalyst” are used interchangeably.
  • the carrier of the present invention comprises a composition represented by general formula (I), general formula (I') or general formula (I"), or has general formula (I), general formula (I') Or the composition shown in general formula (I′′):
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted C 1 -C 5 Linear or branched alkyl;
  • X and Y independently represent halogen;
  • m is 0.1 to 1.9;
  • n is 0.1 to 1.9;
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted C 1 -C 5 Linear or branched alkyl;
  • X is halogen;
  • m is 0.1-1.9;
  • n is 0.1-1.9;
  • m+n 2; 0 ⁇ z ⁇ 0.5;
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted C 1 -C 5 X and Y independently represent halogen;
  • m is 0.1 ⁇ 1.9;
  • n is 0.1 ⁇ 1.9;
  • R 5 and R 7 are the same or different, and are hydrogen or unsubstituted or hydroxy-substituted C 1 -C 8 linear or branched alkyl; R 6 is C 1 -C 8 straight chain Chain or branched alkylene.
  • the above general formula (I) represents a magnesium compound and LB in the specified molar ratio composition.
  • the general formula (I') is represented by and LB in the specified molar ratio composition.
  • the general formula (I") represents A composition consisting of CuYa(OR 4 ) b and LB in the specified molar ratio.
  • the carrier of the present invention comprises the composition represented by the general formula (I"'), or has the composition represented by the general formula (I"'):
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted straight-chain or branched chain of C 1 -C 5
  • X is halogen;
  • m is 0.1-1.9;
  • n is 0.1-1.9;
  • m+n 2; 0 ⁇ z ⁇ 0.5;
  • LB is an amide compound represented by general formula (II'),
  • R 10 is hydrogen, amino or C 1 -C 8 linear or branched alkyl
  • R 11 and R 12 are the same or different, and are hydrogen or C 1 -C 8 linear or branched alkyl .
  • R 1 is a C 1 -C 8 straight or branched chain alkyl group.
  • R 1 is selected from ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-pentyl, isopentyl, n-hexyl, n-octyl and 2-ethylhexyl.
  • R 2 and R 3 are each independently hydrogen, a C 1 -C 3 straight or branched chain alkyl, or a halogen substituted C 1 -C 3 straight or branched chain alkane base.
  • R 2 and R 3 are each independently methyl, ethyl, chloromethyl, chloroethyl, bromomethyl or bromoethyl.
  • R 5 and R 7 are hydrogen or C 1 -C 5 linear or branched alkyl, and R 6 is C 1 -C 5 linear or branched alkylene .
  • R 5 and R 7 are independently hydrogen, methyl, ethyl, isopropyl, n-propyl, tert-butyl, or isobutyl.
  • R 6 is methylene, ethylene or propylene.
  • the compound of formula (II) useful in the present disclosure is selected from the group consisting of ethanolamine, diethanolamine, triethanolamine, N,N-dimethylethanolamine, N,N-diethyl One or more of ethanolamine and N-methyldiethanolamine.
  • R 10 is hydrogen, amino or C 1 -C 5 straight or branched chain alkyl
  • R 11 and R 12 are hydrogen or C 1 -C 5 straight or branched chain the alkyl group.
  • the amide compound represented by the general formula (II') that can be used in the present disclosure is selected from the group consisting of formamide, acetamide, propionamide, N-methylacetamide, N,N-diamide One or more of methylacetamide and carbonamide.
  • the halogen is selected from fluorine, chlorine, bromine and iodine, preferably chlorine.
  • other metal components other than magnesium such as transition metal components, may also be included in the support.
  • the other metal component is one or two selected from iron and copper.
  • the weight percentage of the other metal components in the solid component is 0-1%.
  • the carrier is spherical.
  • spherical as used herein means that the carrier has a quasi-spherical particle morphology, without requiring the carrier to have a perfectly spherical morphology.
  • the carrier has an average particle diameter of 10-100 microns, preferably 30-70 microns, and a particle size distribution of less than 1.2, preferably 0.7-0.9.
  • the present invention provides a method for preparing a carrier for an olefin polymerization catalyst, the method comprising the steps of:
  • X is halogen;
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12 ;
  • R 5 and R 7 are the same or different, and are hydrogen or unsubstituted or hydroxy-substituted straight-chain C 1 -C 8 or branched chain alkyl;
  • R 6 is C 1 -C 8 straight-chain or branched alkylene;
  • R 10 is hydrogen, amino or C 1 -C 8 straight-chain or branched alkyl;
  • R 11 The same as or different from R 12 , it is hydrogen or a straight-chain or branched alkyl group of C 1 -C 8 ;
  • step (b) reacting the solution formed in step (a) with an epoxy compound to directly generate spherical solid particles;
  • step (c) recovering the spherical solid particles formed in step (b).
  • the solid particles are obtained by chemical reaction precipitation, that is, the solid particles are directly precipitated in the original system by chemical reaction during the preparation process, without volatilizing the solvent or changing the system temperature (such as spray drying, reducing the system temperature) and other means to precipitate the reactants to obtain solid particles;
  • the shape of the solid particles (typically spherical) can be achieved without adding inert support materials (such as SiO 2 , metal oxides, etc.) with good particle morphology during the preparation process.
  • inert support materials such as SiO 2 , metal oxides, etc.
  • the method includes the steps of:
  • R 1 is a C 1 -C 12 straight-chain or branched alkyl group
  • R 5 and R 7 are the same or different, and are hydrogen or unsubstituted or hydroxy-substituted C 1 -C 8 straight-chain or branched chain Alkyl
  • R 6 is a linear or branched alkylene group of C 1 -C 8
  • step (b) reacting the solution formed in step (a) with an epoxy compound to directly generate spherical solid particles;
  • step (c) recovering the spherical solid particles formed in step (b).
  • the method includes the steps of:
  • R 1 is a straight-chain or branched alkyl group of C 1 -C 12
  • R 10 is hydrogen, amino or a straight-chain or branched alkyl group of C 1 -C 8
  • R 11 and R 12 are the same or different
  • X is halogen
  • step (b) reacting the solution formed in step (a) with an epoxy compound to directly generate a solid component
  • R 1 is a C 1 -C 8 straight or branched chain alkyl group, preferably R 1 is a C 1 -C 6 straight chain or branched chain alkyl group.
  • R 1 is selected from the group consisting of ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-pentyl, isopentyl, n-hexyl, n-octyl and 2-ethylhexyl .
  • the R 1 OH compound in the step (a) may be an alcohol compound or a mixture of multiple alcohol compounds.
  • Specific compounds such as methanol, ethanol, propanol, isopropanol, n-butanol, isobutanol, amyl alcohol, isoamyl alcohol, n-hexanol, n-octanol, 2-ethyl-1-hexanol.
  • R 5 and R 7 are hydrogen or C 1 -C 5 linear or branched alkyl, and R 6 is C 1 -C 5 linear or branched alkylene .
  • R 5 and R 7 are hydrogen or methyl, ethyl, isopropyl, n-propyl, tert-butyl, isobutyl, and the like.
  • R 6 is methylene, ethylene, propylene, and the like.
  • the compound represented by the general formula (II) is selected from ethanolamine, diethanolamine, triethanolamine, N,N-dimethylethanolamine, N,N-diethylethanolamine and N-methylethanolamine one or more of diethanolamines.
  • R 10 is hydrogen, amino, or C 1 -C 5 straight or branched chain alkyl
  • R 11 and R 12 are hydrogen or C 1 -C 5 straight or branched chain the alkyl group.
  • the amide compound is selected from one or more of formamide, acetamide, propionamide, N-methylacetamide, N,N-dimethylacetamide and carbonamide .
  • the epoxy compound is preferably represented by general formula (III),
  • R 2 and R 3 are the same or different, and are hydrogen or unsubstituted or halogen-substituted C 1 -C 5 straight-chain or branched-chain alkyl groups.
  • R 2 and R 3 are each independently hydrogen, C 1 -C 3 straight or branched chain alkyl or halogen substituted C 1 -C 3 straight or branched chain alkyl.
  • R 2 and R 3 are each independently methyl, ethyl, chloromethyl, chloroethyl, bromomethyl and bromoethyl.
  • a polymer dispersion stabilizer is added during the preparation of the solution, and its weight average molecular weight is greater than 1000, preferably greater than 3000.
  • the magnesium halide of the general formula MgX 2 used in step (a) is one or more selected from the group consisting of magnesium dichloride, magnesium dibromide and magnesium diiodide.
  • a metal halide preferably a reducing metal halide
  • the metal halide can be selected from those of the formula MY a , wherein M is a transition metal, Y is a halogen, and a is 1 or 2.
  • Preferred metal halides are CuCl and FeCl2 .
  • the optional metal halide used in step (a) is selected from the group consisting of ferrous chloride, ferrous bromide, ferrous iodide and hydrates thereof such as ferrous chloride tetrahydrate One or more of iron, preferably ferrous chloride and its hydrate.
  • the optional metal halide used in step (a) is a copper halide, preferably cuprous halide, most preferably cuprous chloride. It has been found that when cuprous halide is used in the above preparation method, the cuprous halide is insoluble (or slightly soluble) in the reaction system, so the mixture formed in step (a) is a suspension. Surprisingly, the particle size of the final carrier particles can be significantly affected by the amount of metal halide added within a certain range.
  • the carrier prepared has an average particle diameter of 10-100 microns, preferably 30-70 microns.
  • the particle size distribution of the prepared support is less than 1.2, preferably 0.7-0.9.
  • the preparation of the solution in said step (a) is carried out at a temperature of 30-160°C, preferably 40-120°C.
  • the R 1 OH compound is added in an amount of 3-30 moles per mole of magnesium, preferably 4-25 moles.
  • the molar ratio of the added amount of the compound represented by the general formula (II) or (II') to the added magnesium halide is 1:200-1:10, preferably 1:200-1: 2, for example, 1:100 to 1:5, preferably 1:50 to 1:50.
  • the step (a) is carried out in a closed container.
  • the order of addition is not specific.
  • the metal halide is added in an amount of 0.001-0.1 moles, preferably 0.003-0.08 moles, per mole of magnesium.
  • an inert dispersion medium may or may not be added during the preparation of the solution in the step (a).
  • the inert dispersion medium can be selected from one or a mixture of liquid aliphatic, aromatic, cycloaliphatic hydrocarbons, silicone oil.
  • the ratio (volume ratio) of the amount of the inert dispersion medium added to the amount of R 1 OH added is 0 to 5:1, preferably 0 to 2:1.
  • examples of the MgX 2 compound described in the step (a) include, but are not limited to, magnesium dichloride, magnesium dibromide, and magnesium diiodide, among which magnesium dichloride is preferred.
  • the MgX 2 compounds can be used alone or in combination.
  • the trace amount of water in each raw material added in the step (a) can participate in the reaction to form the solution.
  • the specific compound of the epoxy compound in the step (b) is ethylene oxide, propylene oxide, butylene oxide, epichlorohydrin, epichlorobutane, Oxybromopropane or epibromobutane etc.
  • the reaction temperature in the step (b) is 30-160°C, preferably 40-120°C.
  • the amount of the ethylene oxide compound added in step (b) is 1-10 moles per mole of magnesium, preferably 2-6 moles.
  • At least one polymer dispersion stabilizer during the preparation of the solution in step (a), and its weight average molecular weight is greater than 1000, preferably greater than 3000, for example up to 2,000,000 , or up to 1,000,000.
  • the amount of the above polymer dispersion stabilizer is 0.1-10% by weight, preferably 0.2-5% by weight, based on the total amount of magnesium compound and R 1 OH compound.
  • the preparation method further comprises step (c) of recovering the obtained solid particles.
  • the solid recovery described in the step (c) refers to the use of solid-liquid separation techniques known in the art, such as filtration, decanting, centrifugal separation and other operations to obtain solid particles, and also includes the spherical carrier particles that are obtained. Hydrocarbon solvent washing and drying.
  • the inert hydrocarbon solvent is preferably a straight-chain or branched-chain liquid alkane and aromatic hydrocarbon with a carbon chain length greater than 4 carbons; specifically, such as: hexane, heptane, octane, decane, toluene, and the like.
  • the preparation method of the carrier comprises:
  • the preparation method of the carrier comprises:
  • the metal halide having a structure of FeY 2 or a metal halide having a structure of CuYc is preferably added in an amount of 0.01-0.1 moles, more preferably 0.01-0.05 moles, per mole of magnesium.
  • the amount of the polymer dispersion stabilizer is 0.1-10% by weight of the total amount of the magnesium halide and the organic alcohol, preferably 0.2-5% by weight.
  • the preparation method of the solid component comprises:
  • a metal halide having a structure of MY a is also added in the above step (1).
  • the preparation method of the spherical carrier comprises:
  • the mixture of magnesium halide, organic alcohol, compound of general formula (II') and at least one polymer dispersion stabilizer is heated to 30-160° C., preferably 40-120° C. °C, the reaction is carried out for 0.1-5 hours, preferably 0.5-2 hours, to form a mixture solution, wherein, based on each mole of magnesium, the amount of the organic alcohol is 3-30 moles, preferably 4-25 moles; the general formula ( The compound represented by II') is added in an amount of 0.01 to 0.5 mol, preferably 0.02 to 0.3 mol.
  • the amount of the polymer dispersion stabilizer is 0.1-10% by weight of the total amount of the magnesium halide and the organic alcohol, preferably 0.2-5% by weight.
  • a metal halide of structure MY a is also optionally added in this step. If the metal halide is added, the metal halide is added in an amount of 0.01-0.1 mole, preferably 0.01-0.05 mole per mole of magnesium.
  • step (3) may further comprise washing and drying the obtained spherical carrier particles with an inert hydrocarbon solvent.
  • the inert hydrocarbon solvent is preferably a straight-chain or straight-chain liquid alkane or aromatic hydrocarbon with a carbon chain length of more than 4 carbons, specifically, for example, hexane, heptane, octane, decane, toluene, and the like.
  • the present invention also provides the solid component prepared by the above preparation method.
  • the solid component is spherical, the average particle diameter is 10-100 microns, preferably 30-70 microns, and the particle size distribution is less than 1.2, preferably 0.7-0.9.
  • the present invention also provides a catalyst component for olefin polymerization, which contains the solid component prepared by the support/solid component and/or the preparation method, a titanium compound and an internal electron donor compound. reaction product.
  • the synthesis of the catalyst component can adopt a known synthesis method, as described in Chinese patent CN1091748, the spherical magnesium-containing composition particles are directly reacted with titanium halide; or as described in Chinese patent CN201310469927, the spherical magnesium-containing composition is first mixed with The alkoxytitanium compound whose structural formula is Ti(OR) 4 is reacted to obtain an intermediate product, which is then reacted with titanium halide to prepare.
  • some internal electron-donor compounds known in the art can be optionally added usually according to the needs of practical application.
  • the present invention also provides a catalyst system for the polymerization of olefins comprising the catalyst component, an alkylaluminum compound, and optionally an external electron donor compound.
  • the present invention also provides a method for olefin polymerization, comprising contacting one or more olefins with the catalyst system under olefin polymerization conditions.
  • the olefin is selected from one or more of ethylene, propylene, 1-butene, 4-methyl-1-pentene and 1-hexene.
  • the present invention has some or all of the following advantages: (1) the solid component of the present invention has an improved particle morphology, which reduces particle adhesion; (2) the catalyst prepared by using the solid component of the present invention as a carrier is in use It has higher stereospecificity during olefin polymerization, especially propylene polymerization or copolymerization; (3) the catalyst prepared with the solid component of the present invention as a carrier has higher strength and less fragmentation; (4) by reacting The reducing metal halide and electron donor compound with specific structure added to the system can adjust the particle size of the carrier without changing the stirring speed, especially to obtain a small particle size without changing the stirring speed. carrier ( ⁇ 40 ⁇ m); (5) increase the stability of the carrier preparation method.
  • Polymer melt index according to the method of ASTM D1238-99, measured at 230°C and 2.16kg.
  • Isotactic index of polymer determined by heptane extraction method (heptane boiling extraction for 6 hours), namely take 2g of dry polymer sample, place it in the extractor and extract with boiling heptane for 6 hours, then , the residue was dried to constant weight, and the ratio of the obtained polymer weight (g) to 2 was the isotactic index.
  • the apparent morphology of the catalyst carrier for olefin polymerization was observed by an optical microscope with a model of Eclipse E200 purchased from Nikon Company, the magnification was 160 times or 400 times, or the XL-30 field emission of the American FEI Company was used. Environmental scanning electron microscope observation.
  • the content of metal elements in the carrier The Agilent ICP-MS 7500CX inductively coupled plasma mass spectrometer of the United States Agilent company was used to test, the carrier was dissolved in concentrated nitric acid, and the test was performed after placing for 12 hours.
  • the 1H-NMR test was performed with an AVANCE 300 nuclear magnetic resonance spectrometer from Bruker, Switzerland. About 100 mg of the sample to be tested was taken into a 2 mL sampling bottle in a glove box with dry nitrogen, and then 1 mL of deuterated toluene and 100 ⁇ L of tri-n-butyl phosphate or triisobutyl phosphate were added to the sampling bottle. The sampling bottle mouth was sealed with a sealing film, placed in a 60°C water bath for 0.5 h and then let stand for several minutes. Then, about one-tenth of the transparent liquid was taken out and added to the NMR tube. In addition, deuterated toluene was added to the NMR tube until the total volume of the liquid in the NMR tube was 0.5 mL, and the prepared samples were tested.
  • the content of electron donors in the carrier Tested by TraceGC Ultra chromatograph and DSQ II mass spectrometer of Thermo Fisher Company in the United States.
  • the chromatographic column is an HP-5 capillary column with a column length of 30m.
  • the sample uses methanol as the solvent, the heating rate is 10 °C/min, and the vaporization temperature is 200 °C.
  • the composition of the solid component particles is as follows:
  • Example 2 The difference between the preparation method and Example 1 is that the formamide is 0.005 mol.
  • the composition of the solid component particles is as follows:
  • Example 1 The difference between the preparation method and Example 1 is only that 2 mmol of ferrous chloride is additionally added. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the main composition of the solid component particles is the same as that of Example 1, and contains 0.046% Fe (weight percentage).
  • Example 4 The difference between the preparation method and Example 4 is only that 9 mmol of ferrous chloride is added. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the main composition of the solid component particles is the same as that of Example 1, and contains 0.59% Fe (weight percentage).
  • Example 1 The difference between the preparation method and Example 1 is only that 5 mmol of cuprous chloride is additionally added. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the main composition of the solid component particles is the same as that of Example 1, and contains 0.038% of Cu (weight percentage).
  • Example 2 The difference between the preparation method and Example 1 is only that 0.015 mol of formamide is replaced with 0.02 mol of N,N-dimethylacetamide.
  • the main composition of the solid component particles is as follows:
  • Example 2 The difference between the preparation method and Example 1 is only that 0.015 mol of formamide is replaced by 0.02 mol of N-methylacetamide.
  • the main composition of the solid component particles is as follows:
  • Example 1 The difference between the preparation method and Example 1 is only that the addition amount of formamide is changed to 0.04mol, and the reaction temperature is 60°C.
  • the composition of the solid component particles is as follows:
  • Example 2 The difference between the preparation method and Example 1 is that 0.015 mol of formamide is replaced by 0.01 mol of carbonamide.
  • the composition of the solid component particles is as follows:
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 1.
  • Example 11 Basically the same as Example 11, except that the solid component particles used were prepared in Example 6.
  • Example 7 Basically the same as Example 10, except that the solid component particles used were prepared in Example 7.
  • the preparation method is the same as that of Example 1, except that the amide compound of general formula (II) is not added.
  • the morphology of the solid component particles is shown in Figures 3A (160 times) and 3B (400 times), and it can be seen from the figures that some solid component particles adhere to form irregular particles.
  • the catalyst preparation and propylene polymerization are the same as those in Example 11, and the polymerization results are shown in Table 1.
  • the present invention improves the particle shape of the carrier by adding the amide compound represented by the general formula (II) during the preparation process of the carrier, and further reduces the Particle sticking.
  • the picture of the catalyst components of the above Example 1 is shown in FIG. 4
  • the picture of the catalyst components of the Comparative Example 1 is shown in FIG. 5 . It can be seen from the figure that the catalyst prepared by adding the solid component particles of the compound represented by the general formula (II) as a carrier is less broken.
  • the preparation method is the same as that in Example 14, except that the amount of ferrous chloride added is 4 mmol. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the preparation method is the same as that in Example 14, except that the addition of ferrous chloride is 8 mmol. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the preparation method is the same as that in Example 14, except that the reaction temperature is 80°C. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the preparation method is the same as that in Example 14, except that the reaction temperature is 60°C.
  • the preparation method is the same as that of Example 18, except that the addition amount of ferrous chloride is 5 mmol. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the preparation method is the same as that of Example 14, except that the addition amount of ferrous chloride tetrahydrate is 0.1 g.
  • the preparation method is the same as that of Example 20, except that the amount of ethanol added is 2.4 mol.
  • the preparation method is the same as in Example 14, except that 2 mmol of triethanolamine is replaced by 4 mmol of N,N dimethylethanolamine. Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the preparation method is the same as that in Example 16, except that the amount of triethanolamine added is 0.01 mol.
  • Characterized by nuclear magnetic resonance, elemental analysis and gas chromatography, the structure of the carrier is as follows:
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 2.
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 2.
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 2.
  • the preparation method was the same as that of Example 19, except that ferrous chloride and the compound described in (II) were not added, and the stirring speed was increased to 1600 rpm.
  • Example 14 The difference from the preparation method of Example 14 is only that 2 mmol of ferrous chloride is replaced by 3 mmol of ferric chloride.
  • Example 14 The difference from the preparation method of Example 14 is only that 2 mmol of ferrous chloride is replaced by 6 mmol of ferric chloride.
  • the picture of the catalyst of the above-mentioned Example 24 is shown in FIG. 7
  • the picture of the catalyst component of Comparative Example 1 is shown in FIG. 5 .
  • the particle morphology is shown in Figure 8A (optical microscope photo, magnified 160 times), Figure 8B (optical microscope photo, magnified 400 times) and Figure 8C (electron microscope image).
  • the preparation method is the same as that of Example 27, except that the amount of triethanolamine added is 4 mmol.
  • the carrier composition is as follows:
  • the preparation method is the same as in Example 27, except that the amount of triethanolamine added is 6 mmol.
  • the carrier composition is as follows:
  • the preparation method is the same as that of Example 27, except that 2 mmol of triethanolamine is replaced with 4 mmol of N,N dimethylethanolamine.
  • the carrier composition is as follows:
  • the preparation method is the same as in Example 27, but 2 mmol of triethanolamine is replaced by 2 mmol of diethanolamine.
  • the carrier composition is as follows:
  • TET tetraethyl titanate
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 3.
  • TET tetraethyl titanate
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70° C., reacted for 1 hour, cooled down, depressurized, discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 3.
  • the present invention improves the particle shape of the carrier due to the addition of the compound represented by the general formula (II) during the preparation process of the carrier, the particle surface is smooth, and further reduces the particle adhesion.
  • the preparation method is the same as that of Example 34, except that the amount of cuprous chloride added is 6 mmol.
  • the carrier composition is as follows:
  • the preparation method is the same as that of Example 34, except that the amount of cuprous chloride added is 0.01 mol.
  • the preparation method is the same as that in Example 36, except that the reaction temperature is 60°C.
  • the carrier composition is as follows:
  • the preparation method is the same as that of Example 36, except that the addition of ethanol is 2.4 mol, and the addition of cuprous chloride is 0.01 mol.
  • the carrier composition is as follows:
  • Example 35 The difference between the preparation method and Example 35 is only that the amount of triethanolamine added is 0.01 mol.
  • the carrier composition is as follows:
  • the preparation method is the same as that in Example 34, except that 2 mmol of triethanolamine is replaced with 4 mmol of N,N dimethylethanolamine.
  • the carrier composition is as follows:
  • the preparation method is the same as that of Example 37, except that the stirring speed is 1200 rpm.
  • the preparation method is the same as that in Example 34, except that triethanolamine is not added.
  • the carrier composition is as follows:
  • the preparation method is the same as that in Example 42, except that the cuprous chloride is 6 mmol, and triethanolamine is not added.
  • the preparation method is the same as that in Example 43, except that the cuprous chloride is 12 mmol, and triethanolamine is not added.
  • the preparation method is the same as in Example 34, except that cuprous chloride is replaced by cupric chloride.
  • the preparation method is the same as that of Example 45, except that the addition amount of cupric chloride is 6 mmol.
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 4.
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 4.
  • the liquid phase bulk polymerization of propylene was carried out in a 5L stainless steel autoclave. Under nitrogen protection, 5ml of triethylaluminum in hexane solution (concentration of 0.5mmol/ml) and 1ml of cyclohexylmethyldimethoxysilane (CHMMS) in hexane solution (concentration of 0.1mmol/ml) were successively added to the reactor. /ml) and 9 mg of the above spherical catalyst component. The autoclave was closed and an amount of hydrogen (standard volume) and 2.3 L of liquid propylene were added. The temperature was raised to 70°C, the reaction was performed for 1 hour, the temperature was lowered, the pressure was relieved, the material was discharged, and the obtained propylene homopolymer was dried and weighed. The results are shown in Table 4.
  • Example 45 and Example 46 show that the effect of adding copper chloride to adjust the particle size of the carrier particles is not obvious.

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Abstract

本发明公开了一种用于制备烯烃聚合催化剂的固体组分及其制备方法和应用。该固体组分其包含：(i)下式(1)所表示的镁化合物，(ii)路易斯碱(LB)，和(iii)任选地，除镁以外的其他金属组分，其中所述路易斯碱是通式(II)所示的化合物或者通式(II')所示的酰胺类化合物。本发明制备的固体组分具有更好的颗粒形态，且以该固体组分作为载体制备的催化剂破碎较少，在用于烯烃聚合特别是丙烯聚合或共聚合时具有更好的立构定向性。

Description

用于制备烯烃聚合催化剂的固体组分及其制备方法和应用
相关申请的交叉引用
本申请要求2020年10月26日提交的CN202011156589.6、CN202011157579.4、CN202011157613.8和CN202011157626.5的优先权和权益，通过引用并且为了所有的目的将所述文件整体结合在本申请中。
技术领域
本发明涉及一种用于制备烯烃聚合催化剂的固体组分(也称为载体)及其制备方法和在烯烃聚合催化剂制备中的应用。
技术背景
用于烯烃聚合的催化剂大多是通过将卤化钛载于活性无水氯化镁上制得的。在这样的方法中，用来制备活性氯化镁的一种方法是将无水α-MgCl 2与醇反应形成加合物，然后再用这种加合物为载体负载卤化钛制备烯烃聚合催化剂固体组分。这种氯化镁的醇合物可通过喷雾干燥、喷雾冷却、高压挤出、高速搅拌、乳化机、超重力旋转床等方法进行制备。如：US4421674、US4469648、WO8707620、WO9311166、US5100849、US6020279、US4399054、EP0395383、US6127304、US6323152、CN1463990、CN1580136等公开了氯化镁醇合物的制备。
另外，研究表明，在氯化镁醇合物二元组分载体制备体系中加入少量给电子体化合物从而形成结构式为MgCl 2·mEtOH·nLB的多组分载体可以提高催化剂的聚合性能，如专利CN101050245中加入的邻苯二甲酸酯类化合物，CN101544710中加入的C，C-二烃氧基烃化合物，CN101550205中加入的聚醚类化合物，CN101486776中加入的聚酯类化合物，CN101215344中加入的邻烷氧基苯甲酸酯类化合物，CN102796127中加入的烷氧基苯甲酰系化合物或羟基苯甲酰系化合物。US2008/0293897教导在氯化镁醇合物载体制备过程中加入除水外的路易斯碱化合物，从而提高了最终催化剂的聚合活性。所述路易斯碱化合物可以为醚、酯和结构式为RX m的化合物，其中R为1-20的碳原子的烷基，X具有-NH 2、-NHR或-OH结构。
活化氯化镁载体也可以烷氧基镁为原料进行制备。CN1016422B公开了一种Z-N催化剂固体组分的制备方法，其是在过渡金属醇盐的存在下，使可溶性二烷基镁与过渡金属卤化物反应，再用液态烃沉淀出固体组分制得。其中采用的二烷氧基镁中的烷氧基为含有6～12个碳原子的线性烷氧基或5～12个碳原子的支链烷氧基，以便能形成溶于液态烃的醇镁溶液，然而这种烷氧基镁难以得到。CN1177868C公开了一种用于烯烃聚合催化剂前体的制备方法，该前体是在截断剂的存在下使烷氧基镁与烷氧基钛反应形成固体配合物而制成的。其中烷氧基镁是二乙氧基镁，烷氧基钛是四乙氧基钛。CN101056894A公开了一种用于丙烯聚合的催化剂，它是通过将二烷氧基镁与卤化钛化合物或卤化硅烷化合物以及内部给电子体在有机溶剂的存在下反应制得。其中二烷氧基镁的通式为Mg(OR) 2，其中R为C1-C6的烷基，并由镁金属与醇反应制得。CN101190953A公开了一种烯烃聚合催化剂 固体组分的制备方法，包括将通式为ClMg(OR)·n(ROH)的含镁配合物，在惰性烃存在下分别与给电子体化合物和四卤化钛反应制得。该含镁配合物由金属镁粉与醇反应制得，其中通式中R是C1-C5的烷基，n为0.1～1.0。
专利申请CN200910235565公开了一种可用作烯烃聚合催化剂载体的化合物及其制备方法，该方法将卤化镁、醇类化合物和惰性分散介质加热形成卤化镁醇合物溶液，之后将该溶液与环氧乙烷类化合物反应生成球形载体。专利申请CN2013104913936教导在上述载体制备过程中加入高分子分散稳定剂，从而在无需加入惰性分散介质的情况下就可得到颗粒形态良好、粒径分布窄的固体颗粒，从而提高了单釜产率，降低了溶剂回收成本。在此基础上，专利申请CN111072804A、CN111072811A、CN107915792A、CN107915793A、CN107915795A、CN109400763A、CN109400778A、CN111072803A相继公开了在上述载体制备过程中加入卤化锌、卤化铬、卤化锰、卤化铁、碱金属卤化物等金属卤化物，以改善载体的颗粒形态和聚合性能。
仍然需要用于制备烯烃聚合催化剂的、显示希望的性能如好的颗粒形态的固体组分/载体。
发明概述
本发明的一个目的是提供一种用于制备烯烃聚合催化剂的固体组分，该固体组分可用作制备烯烃聚合特别是丙烯聚合或共聚合催化剂的载体。本发明的固体组分/载体显示好的颗粒形态，例如没有现有技术所遇到的载体粒子之间粘连的问题。进一步地，以该固体组分为载体制备的催化剂用于烯烃聚合特别是丙烯聚合或共聚合时显示了较高的聚合活性和立体定向性和/或好的氢调敏感性。
本发明的另一个目的是提供一种用于制备烯烃聚合催化剂的固体组分的制备方法。本发明的方法制备工艺简单，制备过程耗能少。
本发明的又一个目的是提供一种烯烃聚合催化剂组分，其含有本发明的载体/固体组分与钛化合物和内给电子体化合物的反应产物。
本发明的又一个目的是提供一种烯烃聚合催化剂体系。
本发明的又一个目的是提供一种烯烃聚合方法。
本发明的其他特征和优点将在下文中详细说明。
附图简要说明
图1A是实施例1制备的固体组分颗粒的形貌光学显微镜照片(放大倍率160倍)。
图1B是实施例1制备的固体组分颗粒的形貌光学显微镜照片(放大倍率400倍)。
图2是实施例4制备的固体组分颗粒的形貌光学显微镜照片(放大倍率160倍)。
图3A是对比例1制备的固体组分的形貌光学显微镜照片(放大倍率160倍)。
图3B是对比例1制备的固体组分的形貌光学显微镜照片(放大倍率400倍)。
图4是实施例1制备的固体催化剂组分颗粒的形貌光学显微镜照片。
图5是对比例1制备的催化剂组分的形貌光学显微镜照片。
图6A是实施例14制备的载体颗粒的形貌光学显微镜照片,放大倍率160。
图6B是实施例14制备的载体颗粒的电镜照片。
图7是实施例24制备的催化剂组分的形貌光学显微镜照片。
图8A是实施例27制备的载体颗粒的形貌光学显微镜照片,放大倍率160。
图8B是实施例27制备的载体颗粒的形貌光学显微镜照片,放大倍率400。
图8C是实施例27制备的载体颗粒的电镜照片。
优选实施方案的详细描述
在第一方面，本发明提供了一种用于制备烯烃聚合催化剂的固体组分，其包含：
(i)下式所表示的镁化合物：
Figure PCTCN2021126397-appb-000001
其中R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；
(ii)路易斯碱(LB)，和
(iii)任选地，除镁以外的其他金属组分，优选地所述其他金属组分是铁和铜中的一种或两种；优选地所述其他金属组分在所述固体组分中的重量百分含量以金属计为0-1％，
其中所述路易斯碱是通式(II)所示的化合物，
Figure PCTCN2021126397-appb-000002
其中，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基；或者
所述路易斯碱是通式(II′)所示的酰胺类化合物，
Figure PCTCN2021126397-appb-000003
其中，R 10为氢、氨基或C 1～C 8的直链或支链的烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基。
在本公开中，术语“用于制备烯烃聚合催化剂的固体组分”和“用于制备烯烃聚合催化剂的载体(或简单地“载体”)”可互换使用。
在一些实施方案中，本发明的载体包含通式(I)、通式(I′)或通式(I″)所示的组合物，或者具有通式(I)、通式(I′)或通式(I″)所示的组成：
Figure PCTCN2021126397-appb-000004
式(I′)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X和Y独立地表示卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<i≤2；0<j≤2；0<k≤2；i+j+k＝3；0<p≤0.1；0<z<0.1；
通式(I)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<z<0.5；
通式(I″)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X和Y独立地表示卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0≤a<2，0<b≤2，a+b＝2；0<q<0.1；0≤z<0.1；
LB为通式(II)所示的化合物，
Figure PCTCN2021126397-appb-000005
通式(II)中，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基。
如本领域技术人员可以理解的，上述通式(I)代表镁化合物
Figure PCTCN2021126397-appb-000006
和LB以指定的摩尔比组成的组合物。同样地，通式(I′)表示由
Figure PCTCN2021126397-appb-000007
Figure PCTCN2021126397-appb-000008
和LB以指定的摩尔比组成的组合物。同样地，通式(I″)表示
Figure PCTCN2021126397-appb-000009
CuYa(OR 4) b以及LB以指定的摩尔比组成的组合物。
在一些实施方案中，本发明的载体包含通式(I″′)所示的组合物，或者具有通式(I″′)所示的组成：
Figure PCTCN2021126397-appb-000010
其中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<z<0.5；LB为通式(II′)所示的酰胺类化合物，
Figure PCTCN2021126397-appb-000011
其中，R 10为氢、氨基或C 1～C 8的直链或支链的烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基。
如本领域技术人员可以理解的，上述通式(I″′)代表镁化合物
Figure PCTCN2021126397-appb-000012
和LB以指定的摩尔比组成的组合物。
在本公开的一些实施方案中，R 1为C 1～C 8的直链或支链的烷基。优选地，R 1选自乙基、正丙基、异丙基、正丁基、异丁基、正戊基、异戊基、正己基、正辛基和2-乙基己基。
在本公开的一些实施方案中，R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基。优选地，R 2和R 3各自独立为甲基、乙基、氯甲基、氯乙基、溴甲基或溴乙基。
在本公开的一些实施方案中，R 5和R 7为氢或C 1～C 5的直链或支链的烷基，R 6为C 1～C 5的直链或支链的亚烷基。在一些实施方案中，R 5和R 7独立地为氢、甲基、乙基、异丙基、正丙基、叔丁基或异丁基。在一些实施方式中，R 6为亚甲基、亚乙基或亚丙基。
在本公开的一些实施方案中，可用于本公开的通式(II)所示的化合物是选自乙醇胺、二乙醇胺、三乙醇胺、N,N-二甲基乙醇胺、N,N-二乙基乙醇胺和N-甲基二乙醇胺中的一种或多种。
在本公开的一些实施方案中，R 10为氢、氨基或C 1～C 5的直链或支链的烷基，R 11和R 12为氢或C 1～C 5的直链或支链的烷基。
在本公开的一些实施方案中，可用于本公开的通式(II′)所示的酰胺类化合物是选自甲酰胺、乙酰胺、丙酰胺、N-甲基乙酰胺、N,N-二甲基乙酰胺和碳酰胺中的一种或多种。
在本申请的上下文中，所述卤素选自氟、氯、溴和碘，优选为氯。
根据本发明，所述载体中还可以包含除镁以外的其他金属组分，例如过渡金属组分。优选地所述其他金属组分是选自铁和铜中的一种或两种。
根据本发明的一些实施方式，所述其他金属组分在所述固体组分中的重量百分含量为0-1％。
根据本发明的一些实施方式，所述载体为球形。在这里使用的术语“球形”是指所述载体具有类球形的颗粒形态，而不要求所述载体具有完美的球形形态。
在一些实施方案中，所述载体的平均颗粒直径为10-100微米，优选为30-70微米，粒径分布小于1.2，优选为0.7-0.9。
在第二方面，本发明提供了一种用于制备烯烃聚合催化剂的载体的方法，该方法包括以下步骤：
(a)将通式MgX 2所示的卤化镁、任选的金属卤化物、通式R 1OH所示的醇类化合物和通式(II)或(II′)所示的化合物反应形成溶液，
Figure PCTCN2021126397-appb-000013
其中，X为卤素；R 1为C 1～C 12的直链或支链的烷基；R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基；R 10为氢、氨基或C 1～C 8的直链或支链的烷基；R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基；
(b)将步骤(a)形成的溶液与环氧化合物反应，直接生成球形固体颗粒；和
(c)回收步骤(b)中形成的球形固体颗粒。
在这里，所述的“直接生成球形固体颗粒”具有如下含义：
(1)所述固体颗粒是通过化学反应析出得到的，即固体颗粒制备过程中通过化学反应在原有体系中直接析出，而不需通过挥发溶剂或改变体系温度(如喷雾干燥、降低体系温度)等手段使反应物析出得到固体颗粒；
(2)所述固体颗粒的形状(典型地球形)的获得无需在制备过程中加入具有良好颗粒形态的惰性载体材料(如SiO 2、金属氧化物等)就可以实现。
在此方面的一个亚方面，所述方法包括以下步骤：
(a)将通式MgX 2所示的卤化镁、任选的结构式为FeY 2的金属卤化物或者任选的结构式为CuYc的金属卤化物与通式R 1OH所示的醇类化合物和通式(II)所示的化合物反应形成溶液，
Figure PCTCN2021126397-appb-000014
其中，R 1为C 1～C 12的直链或支链的烷基，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基，X和Y为卤素，c＝1或2，优选为1；
(b)将步骤(a)形成的溶液与环氧化合物反应，直接生成球形固体颗粒；和
(c)回收步骤(b)中形成的球形固体颗粒。
在此方面的另一个亚方面，所述方法包括以下步骤：
(a)将通式MgX 2所示的卤化镁与通式R 1OH所示的醇类化合物和通式(II′)所示的酰胺类化合物反应形成溶液，
Figure PCTCN2021126397-appb-000015
其中，R 1为C 1～C 12的直链或支链的烷基，R 10为氢、氨基或C 1～C 8的直链或支链的 烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基，X为卤素；
(b)将步骤(a)形成的溶液与环氧化合物反应，直接生成固体组分；和
(c)回收步骤(b)中形成的固体组分。
在此方面的一些实施方案中，R 1为C 1～C 8的直链或支链的烷基，优选地R 1为C 1～C 6的直链或支链的烷基。根据一些具体的实施方案，R 1选自乙基、正丙基、异丙基、正丁基、异丁基、正戊基、异戊基、正己基、正辛基和2-乙基己基。根据本发明的一些优选实施方式，所述步骤(a)中R 1OH化合物可以是一种醇类化合物或多种醇类化合物的混合物。具体的化合物如：甲醇、乙醇、丙醇、异丙醇、正丁醇、异丁醇、戊醇、异戊醇、正己醇、正辛醇、2-乙基-1-已醇。
在此方面的一些实施方案中，R 5和R 7为氢或C 1～C 5的直链或支链的烷基，R 6为C 1～C 5的直链或支链的亚烷基。在一些实施方式中，R 5和R 7为氢或甲基、乙基、异丙基、正丙基、叔丁基、异丁基等。在一些实施方式中，R 6为亚甲基、亚乙基、亚丙基等。根据本发明的一些实施方式，所述通式(II)所示的化合物选自乙醇胺、二乙醇胺、三乙醇胺、N,N-二甲基乙醇胺、N,N-二乙基乙醇胺和N-甲基二乙醇胺中的一种或多种。
在此方面的一些实施方案中，R 10为氢、氨基或C 1～C 5的直链或支链的烷基，R 11和R 12为氢或C 1～C 5的直链或支链的烷基。根据本发明的一些实施方式，所述酰胺类化合物选自甲酰胺、乙酰胺、丙酰胺、N-甲基乙酰胺、N,N-二甲基乙酰胺和碳酰胺中的一种或多种。
在此方面的一些实施方案中，所述环氧化合物优选如通式(III)所示，
Figure PCTCN2021126397-appb-000016
其中R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基。优选地，R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基。优选地，R 2和R 3各自独立为甲基、乙基、氯甲基、氯乙基、溴甲基和溴乙基。
在此方面的一些实施方案中，步骤(a)中，在溶液的制备过程中加入高分子分散稳定剂，其重均分子量大于1000，优选大于3000。
在此方面的一些实施方案中，步骤(a)中使用的通式MgX 2所示的卤化镁是选自二氯化镁、二溴化镁和二碘化镁中的一种或多种。
在此方面的一些实施方案中，在所述步骤(a)中可加入金属卤化物，优选具有还原性的金属卤化物。例如，金属卤化物可以选自结构式为MY a的那些，其中M为过渡金属，Y为卤素，a为1或2。在一些具体实施方案中，M为铜,并且a＝1。在另外的具体实施方案中，M为铁，并且a＝2。优选的金属卤化物为CuCl和FeCl 2。
在此方面的一些实施方案中，步骤(a)中使用的任选的金属卤化物是选自氯化亚铁、溴化亚铁、碘化亚铁以及它们的水合物如四水合氯化亚铁中的一种或多种，优选氯化亚铁及其水合物。
在此方面的一些实施方案中，步骤(a)中使用的任选的金属卤化物为铜卤化物，优 选为卤化亚铜，最优选为氯化亚铜。已经发现，当在上述制备方法中采用卤化亚铜时，所述卤化亚铜不溶(或微溶)于反应体系中，所以在步骤(a)中所形成的混合物为悬浊液。令人意想不到的是，最终得到的载体颗粒的粒径在一定范围内可以受金属卤化物的加入量显著影响。
在此方面的一些实施方案中，所制备的载体的平均颗粒直径为10-100微米，优选为30-70微米。
在此方面的一些实施方案中，所制备的载体的粒径分布小于1.2，优选为0.7-0.9。
在此方面的一些实施方案中，所述步骤(a)中所述溶液的制备在30-160℃温度下进行，优选40-120℃。根据本发明的一些实施方式，R 1OH化合物的加入量以每摩尔镁计为3-30摩尔，优选4-25摩尔。根据本发明的一些实施方式，通式(II)或(II′)所示的化合物的加入量与所加入的卤化镁的摩尔比为1：200～1：10，优选1：200～1：2，例如为1：100～1：5，优选1：50～1：50。根据本发明的一些优选实施方式，所述步骤(a)在密闭的容器中实施。根据本发明的一些优选实施方式，所述步骤(a)，在溶液的制备过程中，加料顺序不分先后。
在此方面的一些实施方案中，所述金属卤化物的加入量以每摩尔镁计为0.001-0.1摩尔，优选0.003-0.08摩尔。
根据本发明的一些实施方式，所述步骤(a)中在溶液的制备过程中可加入或不加入惰性分散介质。所述惰性分散介质可选用液体脂族、芳族、环脂族的烃类、硅油的一种或其混合物。加入的惰性分散介质的量与R 1OH加入量之比(体积比)为0～5：1，优选0～2：1。
根据本发明的一些优选实施方式，所述步骤(a)中所述的MgX 2化合物的实例包括但不限于二氯化镁、二溴化镁、二碘化镁，其中优选二氯化镁。所述的MgX 2化合物可以单独或混合使用。
根据本发明的一些优选实施方式，所述步骤(a)中加入的各原料中的微量水可参与形成溶液的反应。
根据本发明的一些优选实施方式，所述步骤(b)中的环氧化合物的具体化合物为环氧乙烷、环氧丙烷、环氧丁烷、环氧氯丙烷、环氧氯丁烷、环氧溴丙烷或环氧溴丁烷等。
根据本发明的一些优选实施方式，所述步骤(b)中反应温度为30-160℃，优选40-120℃。
根据本发明的一些优选实施方式，步骤(b)中环氧乙烷类化合物加入量以每摩尔镁计为1-10摩尔，优选2-6摩尔。
为了得到颗粒形态更好的粒子，优选步骤(a)中在溶液的制备过程中加入至少一种高分子分散稳定剂，其重均分子量大于1000，优选大于3000，例如最高达2，000，000，或者最高达1，000，000。具体可选用聚丙烯酸盐、苯乙烯-马来酸酐共聚物、聚苯乙烯磺酸盐、萘磺酸甲醛缩合物、缩合烷基苯基醚硫酸酯、缩合烷基苯酚聚氧乙烯醚磷酸酯、氧基烷基丙烯酸酯共聚物改性聚乙撑亚胺、1-十二-4-乙烯吡啶溴化物的聚合物、聚乙烯基苄基三甲胺盐、聚乙烯醇、聚丙烯酰胺、环氧乙烷环氧丙烷嵌段共聚物、聚乙烯吡咯烷酮、聚乙烯吡咯烷酮醋酸乙烯共聚物、聚乙二醇、聚氧乙烯缩合烷基苯基醚、聚甲基丙烯酸烷基酯类中的一种或其混合物。优选聚乙烯吡咯烷酮、聚乙烯吡咯烷酮醋酸乙烯酯共聚物和聚乙二醇中的至少一种。
根据本发明的一些优选实施方式，上述高分子分散稳定剂的用量为镁化合物和R 1OH化合物总用量的0.1～10％(重量)，优选0.2～5％(重量)。
根据本发明，所述制备方法还包括步骤(c)回收所得固体颗粒。所述步骤(c)中所述的固体回收是指采用本领域公知的固-液分离技术，如过滤、滗析、离心分离等操作得到固体颗粒，同时也包括将得到的球形载体颗粒经惰性烃类溶剂洗涤、干燥。其中惰性烃类溶剂优选碳链长度大于4个碳的直链或支链液态烷烃、芳烃；具体如：己烷、庚烷、辛烷、癸烷、甲苯等。
在一种优选的实施方式中，所述载体的制备方法包括：
(1)在密闭的容器中，在至少一种高分子分散稳定剂的存在下，将卤化镁MgX 2、有机醇R 1OH、任选的结构为FeY 2的金属卤化物或者任选的结构为CuYc的金属卤化物及通式(II)的化合物的混合物在30-160℃(优选40-120℃)下反应0.1-5小时(优选0.5-2小时)形成溶液；
(2)将所述溶液与上述式(Ⅲ)所示的环氧烷类化合物在30-160℃(优选40-120℃)下反应0.1-5小时(优选0.2-1小时)，直接析出固体颗粒；
(3)通过固液分离技术回收所述固体颗粒得到球形载体。
在一种更优选的实施方式中，所述载体的制备方法包括：
(1)在密闭的容器中，在搅拌下将卤化镁、有机醇、任选的结构为FeY 2的金属卤化物或者任选的结构为CuYc的金属卤化物、通式(Ⅱ)的化合物和至少一种高分子分散稳定剂的混合物加热升温到30-160℃，优选40-120℃，反应0.1-5小时，优选0.5-2小时，形成混合物溶液，其中，以每摩尔镁计，所述有机醇的用量为3-30摩尔，优选为4-25摩尔；所述通式(Ⅱ)所示的化合物的加入量0.005～0.1摩尔，优选0.005～0.05摩尔。结构为FeY 2的金属卤化物或者结构为CuYc的金属卤化物的加入量以每摩尔镁计优选为0.01-0.1摩尔，更优选0.01-0.05摩尔。所述高分子分散稳定剂的用量为所述卤化镁和所述有机醇总用量的0.1-10重量％，优选为0.2-5重量％。
(2)在搅拌下，向上述混合物溶液中加入上述式(Ⅲ)所示的环氧烷类化合物，在30-160℃(优选40-120℃)下反应0.1-5小时，优选0.2-1小时，直接形成固体颗粒，其中，以每摩尔镁计，所述环氧烷类化合物的用量为1-10摩尔，优选2-6摩尔；
(3)通过固液分离技术回收所述固体颗粒得到球形载体。
在一种优选的实施方式中，所述固体组分的制备方法包括：
(1)在密闭的容器中，在至少一种高分子分散稳定剂的存在下，将卤化镁MgX 2、有机醇R 1OH及通式(II′)的化合物的混合物在30-160℃(优选40-120℃)下反应0.1-5小时(优选0.5-2小时)形成溶液；
(2)将所述溶液与上述式(Ⅲ)所示的环氧烷类化合物在30-160℃(优选40-120℃)下反应0.1-5小时(优选0.2-1小时)，直接析出固体颗粒；
(3)通过固液分离技术回收所述固体颗粒得到球形载体。
在一种优选的实施方式中，在上述步骤(1)中还加入结构为MY a的金属卤化物。
在一种更优选的实施方式中，所述球形载体的制备方法包括：
(1)在密闭的容器中，在搅拌下将卤化镁、有机醇、通式(II′)的化合物和至少一种 高分子分散稳定剂的混合物加热升温到30-160℃，优选40-120℃，反应0.1-5小时，优选0.5-2小时，形成混合物溶液，其中，以每摩尔镁计，所述有机醇的用量为3-30摩尔，优选为4-25摩尔；所述通式(II′)所示的化合物的加入量0.01～0.5摩尔，优选0.02～0.3摩尔。所述高分子分散稳定剂的用量为所述卤化镁和所述有机醇总用量的0.1-10重量％，优选为0.2-5重量％。在该步骤中还任选地加入结构为MY a的金属卤化物。如果加入所述金属卤化物，则该金属卤化物的加入量以每摩尔镁计为0.01-0.1摩尔，优选0.01-0.05摩尔。
(2)在搅拌下，向上述混合物溶液中加入上述式(Ⅲ)所示的环氧烷类化合物，在30-160℃(优选40-120℃)下反应0.1-5小时，优选0.2-1小时，直接形成固体颗粒，其中，以每摩尔镁计，所述环氧烷类化合物的用量为1-10摩尔，优选2-6摩尔；
(3)通过固液分离技术回收所述固体颗粒得到球形载体。
在上述优选实施方式中，回收固体颗粒的过程可以根据本领域的常规固液分离技术实施，例如可以采用过滤、滗析、离心分离等方式实施。而且，步骤(3)还可以包括将得到的球形载体颗粒用惰性烃类溶剂进行洗涤和干燥。所述惰性烃类溶剂优选为碳链长度大于4个碳的直链或直链液态烷烃、芳烃，具体地，例如可以为己烷、庚烷、辛烷、癸烷、甲苯等。
本发明还提供了上述制备方法制备的固体组分。根据本发明的一些实施方式，所述固体组分为球形，平均颗粒直径为10-100微米，优选为30-70微米，粒径分布小于1.2，优选为0.7-0.9。
本发明还提供了一种用于烯烃聚合的催化剂组分，其含有由所述的载体/固体组分和/或所述的制备方法制备的固体组分与钛化合物和内给电子体化合物的反应产物。催化剂组分的合成可采用公知的合成方法，如中国专利CN1091748所描述的，将球形含镁组合物颗粒直接与卤化钛反应；或采用中国专利CN201310469927所描述的，将球形含镁组合物先与结构式为Ti(OR) 4的烷氧基钛化合物反应得到中间产物，再与卤化钛反应进行制备。在上述催化剂制备过程中，通常根据实际应用的需要可任选地加入一些本行业公知的内给电子体化合物。
本发明还提供了用于烯烃聚合的催化剂体系，其含有所述的催化剂组分、烷基铝化合物以及任选的外给电子体化合物。
本发明还提供了一种烯烃聚合方法，包括在烯烃聚合条件下，将一种或多种烯烃与所述的催化剂体系接触。在本发明的实施方式中，所述烯烃的通式通式为CH 2＝CHR，其中R为氢或C 1-C 7烷基。优选地，所述烯烃选自乙烯、丙烯、1-丁烯、4-甲基-1-戊烯和1-己烯中的一种或多种。
本发明具有以下部分或全部优点：(1)本发明所述组成的固体组分具有改进的颗粒形态，减少了粒子粘连；(2)以本发明所述固体组分为载体制备的催化剂在用于烯烃聚合特别是丙烯聚合或共聚合时具有更高的立构定向性；(3)以本发明所述固体组分为载体制备的催化剂强度更高，破碎更少；(4)通过在反应体系中加入的具有还原性的金属卤化物和具有特定结构的给电子体化合物，可在不改变搅拌转速的情况下实现对载体粒径的调节，特别是在不改变搅拌转速下得到小粒径载体(<40μm)；(5)增加载体制备方法的稳定性。
具体实施方式
下面实施例进一步描述本发明，并不用来限制本发明的范围。
测试方法：
1、聚合物熔融指数：根据ASTM D1238-99的方法，在230℃、2.16kg条件下测定。
2、聚合物等规指数：采用庚烷抽提法测定(庚烷沸腾抽提6小时)，即取2g干燥的聚合物样品，置于抽提器中用沸腾庚烷抽提6小时，之后，将剩余物干燥至恒重，所得聚合物重量(g)与2的比值即为等规指数。
3、粒径分布测试：载体颗粒的平均粒径和粒度分布用Masters Sizer 2000粒度仪(由Malvern Instruments Ltd生产制造)测定，分散介质为正己烷。粒径分布值SPAN＝(D90-D10)/D50。
4、烯烃聚合用催化剂载体的表观形貌通过商购自Nikon公司的型号为Eclipse E200的光学显微镜进行观察，放大倍率为160倍或者400倍，或者采用美国FEI公司的XL-30型场发射环境扫描电镜观察。
5、载体中金属元素含量：采用美国Agilent公司的Agilent ICP-MS 7500CX电感耦合等离子体质谱仪测试，载体用浓硝酸溶解，放置12h后测试。
6、催化剂的活性＝所得到的聚合物的重量/所使用的催化剂的重量。
7、1H-NMR测试采用瑞士Bruker公司的AVANCE 300核磁共振谱仪进行。在通有干燥氮气的手套箱中取被测样品约100mg放入2mL取样瓶中，之后向取样瓶中加入1mL氘代甲苯和100μL磷酸三正丁酯或磷酸三异丁酯。将取样瓶口用密封膜密封，放入60℃水浴中超声0.5h后静置数分钟。之后取出大约十分之一的透明液体加入到核磁管中，另外再向核磁管中补加氘代甲苯至核磁管中的液体总体积为0.5mL，将配好的样品进行测试。
8、载体中给电子体含量：采用美国Thermo Fisher公司的TraceGC Ultra色谱仪和DSQⅡ型质谱仪测试，色谱柱为HP-5毛细管柱，柱长30m。试样以甲醇为溶剂，升温速率为10℃/min，汽化温度200℃。
A-1、球形载体的制备
实施例1
在1.0L的反应釜中，依次加入聚乙烯吡咯烷酮(PVP,重均分子量＝58000)1.6g，乙醇2.8mol，氯化镁0.2mol，甲酰胺0.015mol，在搅拌下(450rpm)升温至70℃。恒温反应1小时后，加入环氧氯丙烷0.6mol，维持温度反应0.5小时，滤去液体，用已烷洗涤固体5次，真空干燥，得到固体组分颗粒。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的组成如下：
Figure PCTCN2021126397-appb-000017
固体组分颗粒的粒径分布为D50＝63.5μm，Span＝0.67，颗粒形态见图1A(160倍)和1B(400倍)。
实施例2
制备方法同实施例1的不同之处仅在于，甲酰胺0.03mol，反应温度80℃。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的组成如下：
Figure PCTCN2021126397-appb-000018
固体组分颗粒的粒径分布D50＝45.2μm，Span＝0.65。
实施例3
制备方法同实施例1的不同之处仅在于，甲酰胺0.005mol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的组成如下：
Figure PCTCN2021126397-appb-000019
载体粒径分布D50＝78.5μm，Span＝0.67。
实施例4
制备方法同实施例1的不同之处仅在于，额外加入氯化亚铁2mmol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的主体组成与实施例1相同，并含有0.046％的Fe(重量百分含量)。
固体组分颗粒的粒径分布D50＝61.4μm，Span＝0.69，颗粒形态见图2。
实施例5
制备方法同实施例4的不同之处仅在于，加入氯化亚铁9mmol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的主体组成与实施例1相同，并含有0.59％的Fe(重量百分含量)。
固体组分颗粒的粒径分布D50＝47.1μm，Span＝0.76。
实施例6
制备方法同实施例1的不同之处仅在于，额外加入氯化亚铜5mmol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的主体组成与实施例1相同，并含有0.038％的Cu(重量百分含量)。
固体组分颗粒的粒径分布D50＝53.1μm，Span＝0.68。
实施例7
制备方法同实施例1的不同之处仅在于，将甲酰胺0.015mol替换为N,N-二甲基乙酰胺0.02mol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的主体组成如下：
Figure PCTCN2021126397-appb-000020
固体组分颗粒的粒径分布D50＝65.1μm，Span＝0.65。
实施例8
制备方法同实施例1的不同之处仅在于，将甲酰胺0.015mol替换为N-甲基乙酰胺0.02mol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的主体组成如下：
Figure PCTCN2021126397-appb-000021
固体组分颗粒的粒径分布D50＝57.8μm，Span＝0.67。
实施例9
制备方法同实施例1的不同之处仅在于，将甲酰胺的加入量改为0.04mol，反应温度60℃。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的组成如下：
Figure PCTCN2021126397-appb-000022
固体组分颗粒的粒径分布D50＝43.6μm，Span＝0.66。
实施例10
制备方法同实施例1的不同之处仅在于，将甲酰胺0.015mol替换为碳酰胺0.01mol。通过核磁共振、元素分析及气相色谱表征，固体组分颗粒的组成如下：
Figure PCTCN2021126397-appb-000023
固体组分颗粒的粒径分布D50＝65.3μm，Span＝0.65。
B-1、球形催化剂组分的制备
实施例11
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g实施例1制备的固体组分颗粒分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷 (CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表1。
实施例12
与实施例11基本相同，不同之处仅在于，所使用的固体组分颗粒为实施例6制备。
实施例13
与实施例10基本相同，不同之处仅在于，所使用的固体组分颗粒为实施例7制备。
比较例1
球形载体的制备
与实施例1制备方法相同，只是不加入通式(II)的酰胺类化合物。固体组分颗粒形态见图3A(160倍)和3B(400倍)，从图中可以看出有部分固体组分颗粒出现粘连形成异形颗粒。
催化剂制备及丙烯聚合同实施例11，聚合结果见表1。
从上述固体组分的粒径分布及附图的结果可以看出，本发明在载体制备过程中由于加入通式(II)所示的酰胺类化合物，从而改善了载体的颗粒形态，进一步减少了粒子粘连。
表1 实施例载体制备催化剂的性能
Figure PCTCN2021126397-appb-000024
从表1的结果可以看出，载体制备过程中加入酰胺类化合物可提高催化剂的立构定向性，且对催化剂的聚合活性基本没有影响。
上述实施例1的催化剂组分图片见图4，比较例1的催化剂组分图片见图5。从图中可以看出，加入通式(II)所示的化合物的固体组分颗粒作为载体制备的催化剂破碎较少。
A-2、球形载体的制备
实施例14
在1.0L的反应釜中，依次加入聚乙烯吡咯烷酮(PVP,重均分子量＝58000)1.6g，乙醇2.8mol，氯化镁0.2mol，氯化亚铁2mmol，三乙醇胺2mmol，在搅拌下(450rpm)升温至70℃。恒温反应1小时后，加入环氧氯丙烷0.6mol，维持温度反应0.5小时，滤去液体，用已烷洗涤固体5次，真空干燥，得到固体组分颗粒。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000025
载体粒径分布D50＝71.1μm，Span＝0.65，颗粒形态见图6A(光学显微镜照片，160倍)和图6B(电镜照片)。
实施例15
制备方法同实施例14，不同之处仅在于氯化亚铁加入量为4mmol。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000026
载体粒径分布D50＝68.2μm，Span＝0.67。
实施例16
制备方法同实施例14，不同之处仅在于氯化亚铁加入量为8mmol。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000027
载体粒径分布D50＝39.8μm，Span＝0.68。
实施例17
制备方法同实施例14，不同之处仅在于反应温度为80℃。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000028
载体粒径分布D50＝72.2μm，Span＝0.65。
实施例18
制备方法同实施例14，不同之处仅在于反应温度为60℃。
载体粒径分布D50＝38.8μm，Span＝0.66。
实施例19
制备方法同实施例18，不同之处仅在于氯化亚铁加入量为5mmol。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000029
载体粒径分布D50＝35.4μm，Span＝0.66。
实施例20
制备方法同实施例14，不同之处仅在于四水合氯化亚铁加入量为0.1g。
载体粒径分布D50＝81.6μm，Span＝0.59。
实施例21
制备方法同实施例20，不同之处仅在于乙醇加入量为2.4mol。
载体粒径分布D50＝73.5μm，Span＝0.67。
实施例22
制备方法同实施例14，不同之处仅在于三乙醇胺2mmol替换为N，N二甲基乙醇胺4mmol。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000030
载体粒径分布D50＝69.5μm，Span＝0.64。
实施例23
制备方法同实施例16，不同之处仅在于三乙醇胺加入量为0.01mol。通过核磁共振、元素分析及气相色谱表征，载体结构如下：
Figure PCTCN2021126397-appb-000031
载体粒径分布D50＝53.2μm，Span＝0.68。
B-2、球形催化剂组分的制备
实施例24
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例14制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷 (CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表2。
实施例25
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例15制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表2。
实施例26
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例21制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表2。
比较例2
与实施例19制备方法相同，不加入氯化亚铁和(Ⅱ)所述化合物，搅拌转速提高至1600rpm。载体粒径分布D50＝35.4μm，Span＝0.9。
比较例3
与实施例14制备方法的不同之处仅在于氯化亚铁2mmol替换为三氯化铁3mmol。载体粒径分布D50＝76.5μm，Span＝0.68。观察到有部分载体颗粒出现粘连形成异形颗粒。
比较例4
与实施例14制备方法的不同之处仅在于氯化亚铁2mmol替换为三氯化铁6mmol。载体粒径分布D50＝72.5μm，Span＝0.67。
比较例5
与实施例14制备方法的不同之处仅在于不加入三乙醇胺。载体粒径分布D50＝71.0μm，Span＝0.67。观察到表面粗糙且还有少量粘连。
从上述载体的粒径分布及附图的结果可以看出，本发明在载体制备过程中加入氯化亚铁，可明显改善载体的颗粒形态，减少粒子粘连，并且随着氯化亚铁加入量的增多，载体粒径明显减小(实施例14-16)，并在低速搅拌下就可得到小粒径载体(见实施例19)。当不加入氯化亚铁时，即使搅拌转速提高到1600rpm，载体的粒径仍然有35μm，且粒径分布明显变宽(见比较例2)。比较例3、比较例4表明加入三氯化铁对载体颗粒粒径的调节作用并不明显。比较例5说明只有与通式(Ⅱ)所述化合物复合使用，氯化亚铁对载体粒形的改善作用才更明显。
表2 实施例载体制备催化剂的性能
Figure PCTCN2021126397-appb-000032
上述实施例24的催化剂图片见图7，比较例1的催化剂组分的图片见图5。
从表2及图7、图5的结果可以看出，由本发明的球形载体制备的催化剂组分用于丙烯聚合时，具有较高的聚合活性和立体定向性，同时催化剂表面无裂纹，且破碎较少。
A-3、球形载体的制备
实施例27
在1.0L的反应釜中，依次加入聚乙烯吡咯烷酮(PVP,重均分子量＝58000)1.6g，乙醇2.8mol，氯化镁0.2mol，三乙醇胺2mmol，在搅拌下(450rpm)升温至70℃。恒温反应1小时后，加入环氧氯丙烷0.6mol，维持温度反应0.5小时，滤去液体，用已烷洗涤固体5次，真空干燥，得到固体组分颗粒。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000033
载体粒径分布D50＝59.9μm，Span＝0.66。颗粒形态见图8A(光学显微镜照片，放大160倍)、图8B(光学显微镜照片，放大400倍)和图8C(电镜图)。
实施例28
制备方法同实施例27，不同之处仅在于三乙醇胺加入量为4mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000034
载体粒径分布D50＝66μm，Span＝0.65。
实施例29
制备方法同实施例27，不同之处仅在于三乙醇胺加入量为6mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000035
载体粒径分布D50＝86μm，Span＝0.73。
实施例30
制备方法同实施例27，不同之处仅在于将三乙醇胺2mmol替换为N，N二甲基乙醇胺4mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000036
载体粒径分布D50＝58.6μm，Span＝0.65。
实施例31
制备方法同实施例27，但是将三乙醇胺2mmol替换为二乙醇胺2mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000037
载体粒径分布D50＝58.6μm，Span＝0.65。
B-3、球形催化剂组分的制备
实施例32
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例27制备的 载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表3。
实施例33
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例30制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表3。
从上述载体的粒径分布及附图的结果可以看出，本发明在载体制备过程中由于加入通式(II)所示的化合物，从而改善了载体的颗粒形态，粒子表面光滑，且进一步减少了粒子粘连。
表3 实施例载体制备催化剂的性能
Figure PCTCN2021126397-appb-000038
Figure PCTCN2021126397-appb-000039
从表3的结果可以看出，载体制备过程中加入醇胺类化合物可提高催化剂的氢调敏感性。
A-4、烯烃聚合催化剂载体的制备
实施例34
在1.0L的反应釜中，依次加入聚乙烯吡咯烷酮(PVP,重均分子量＝58000)1.6g，乙醇2.8mol，氯化镁0.2mol，氯化亚铜3mmol，三乙醇胺2mmol，在搅拌下(搅拌转速450rpm)升温至70℃。恒温反应1小时后，加入环氧氯丙烷0.6mol，维持温度反应0.5小时，滤去液体，用已烷洗涤固体5次，真空干燥，得到固体组分颗粒。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000040
载体粒径分布D50＝68.2μm，Span＝0.64。
实施例35
制备方法同实施例34，不同之处仅在于氯化亚铜加入量为6mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000041
载体粒径分布D50＝54.8μm，Span＝0.64。
实施例36
制备方法同实施例34，不同之处仅在于氯化亚铜加入量0.01mol。载体粒径分布D50＝45.4μm，Span＝0.64。
实施例37
制备方法同实施例36，不同之处仅在于反应温度为60℃。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000042
载体粒径分布D50＝31μm，Span＝0.64。
实施例38
制备方法同实施例36，不同之处仅在于乙醇加入量为2.4mol，氯化亚铜加入量为 0.01mol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000043
载体粒径分布D50＝36.2μm，Span＝0.64。
实施例39
制备方法同实施例35的不同之处仅在于三乙醇胺加入量为0.01mol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000044
载体粒径分布D50＝57.8μm，Span＝0.7。
实施例40
制备方法同实施例34，不同之处仅在于将三乙醇胺2mmol替换为N，N二甲基乙醇胺4mmol。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000045
载体粒径分布D50＝52.8μm，Span＝0.64。
实施例41
制备方法同实施例37，不同之处仅在于搅拌转速为1200rpm。
载体粒径分布D50＝24.5μm，Span＝0.64。
实施例42
制备方法同实施例34，不同之处仅在于不加入三乙醇胺。通过核磁共振、元素分析及气相色谱表征，载体组成如下：
Figure PCTCN2021126397-appb-000046
载体粒径分布D50＝60.4μm，Span＝0.63。
实施例43
制备方法同实施例42，不同之处仅在于氯化亚铜6mmol，不加入三乙醇胺。
载体粒径分布D50＝57.2μm，Span＝0.64。
实施例44
制备方法同实施例43，不同之处仅在于氯化亚铜12mmol，不加入三乙醇胺。
载体粒径分布D50＝35.3μm，Span＝0.67。
实施例45
制备方法同实施例34，不同之处仅在于氯化亚铜替换为氯化铜。
Figure PCTCN2021126397-appb-000047
载体粒径分布D50＝62.5μm，Span＝0.69。
实施例46
制备方法同实施例45，不同之处仅在于氯化铜加入量为6mmol。
载体粒径分布D50＝60.2μm，Span＝0.68。
B-4、球形催化剂组分的制备
实施例47
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例34制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表4。
实施例48
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例40制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入 上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表4。
实施例49
(1)制备中间反应产物
在300mL带有机械搅拌的玻璃反应瓶中，氮气气氛下，将10g上述实施例42制备的载体分散在100ml己烷中，冷却至-10℃，维持0.5hr，加入钛酸四乙酯(TET)2.5ml(TET/Mg摩尔比＝0.2)，缓慢升温至60℃，维持0.5hr。滤去液体，用己烷洗涤三次，真空干燥后得到中间产物。
(2)催化剂组分制备
在惰性气氛下，300mL的玻璃反应瓶中，加入100ml四氯化钛，冷却至-20℃，加入上述(1)制备的中间产物8g，升温至110℃。在升温过程中加入邻苯二甲酸二异丁酯1.5ml，滤去液体，用四氯化钛洗涤二次，用己烷洗涤三次，真空干燥后得球形催化剂组分。
C、丙烯聚合
丙烯液相本体聚合是在5L的不锈钢高压反应釜中进行。在氮气保护下向反应釜中依次加入5ml三乙基铝的己烷溶液(浓度为0.5mmol/ml)、1ml环己基甲基二甲氧基硅烷(CHMMS)的己烷溶液(浓度为0.1mmol/ml)和9mg上述球形催化剂组分。关闭高压釜，加入一定量氢气(标准体积)和2.3L的液体丙烯。升温至70℃，反应1小时，降温，卸压，出料，将所得丙烯均聚物干燥后称重。结果见表4。
从上述载体的粒径分布及附图的结果可以看出，本发明在载体制备过程中加入氯化亚铜，可明显改善载体的颗粒形态，减少粒子粘连，并且随着氯化亚铜加入量的增多，载体粒径明显减小(实施例34-36，42-44)；特别是与通式(II)所示的胺类化合物复合使用，载体的表面更光滑，球形度更好，对粒子粒径调节作用更明显，并在低速搅拌下就可得到小粒径载体(见实施例37)。当增加搅拌转速时，载体的粒径可进一步减小至25μm，并且具有窄的粒径分布(见实施例41)。当不加入氯化亚铜时，即使搅拌转速提高到1600rpm，载体的粒径仍然有35μm，且粒径分布明显变宽(见对比例2)。实施例45、实施例46表明加入氯化铜对载体颗粒粒径的调节作用并不明显。
表4 实施例载体制备催化剂的性能
Figure PCTCN2021126397-appb-000048
Figure PCTCN2021126397-appb-000049
从表4的结果可以看出，载体制备过程中加入醇胺类化合物可提高催化剂的氢调敏感性，且对催化剂的聚合活性基本没有影响。
应当注意的是，以上所述的实施例仅用于解释本发明，并不构成对本发明的任何限制。通过参照典型实施例对本发明进行了描述，但应当理解为其中所用的词语为描述性和解释性词汇，而不是限定性词汇。可以按规定在本发明权利要求的范围内对本发明作出修改，以及在不背离本发明的范围和精神内对本发明进行修订。尽管其中描述的本发明涉及特定的方法、材料和实施例，但是并不意味着本发明限于其中公开的特定例，相反，本发明可扩展至其他所有具有相同功能的方法和应用。

Claims (15)

  1. 一种烯烃聚合催化剂的载体，其包含：
    (i)下式(1)所表示的镁化合物：
    Figure PCTCN2021126397-appb-100001
    其中R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；
    (ii)路易斯碱(LB)，和
    (iii)任选地，除镁以外的其他金属组分，优选地所述其他金属组分是铁和铜中的一种或两种；优选地所述其他金属组分在所述固体组分中的重量百分含量以金属计为0-1％，
    其中所述路易斯碱是通式(II)所示的化合物，
    Figure PCTCN2021126397-appb-100002
    其中，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基；或者
    是通式(II′)所示的酰胺类化合物，
    Figure PCTCN2021126397-appb-100003
    其中，R 10为氢、氨基或C 1～C 8的直链或支链的烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基。
  2. 权利要求1的烯烃聚合催化剂载体，其包含通式(I)、通式(I′)或通式(I″)所示的组合物：
    Figure PCTCN2021126397-appb-100004
    Figure PCTCN2021126397-appb-100005
    式(I′)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X和Y独立地表示卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<i≤2；0<j≤2；0<k≤2；i+j+k＝3；0<p≤0.1；0<z<0.1；
    通式(I)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<z<0.5；
    通式(I″)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X和Y独立地表示卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0≤a<2，0<b≤2，a+b＝2；0<q<0.1；0≤z<0.1；
    LB为通式(II)所示的化合物，
    Figure PCTCN2021126397-appb-100006
    通式(II)中，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基。
  3. 根据权利要求2所述的烯烃聚合催化剂载体，其具有以下特征至少之一：
    -通式(I)、通式(I′)或通式(I″)中，R 1为C 1～C 8的直链或支链的烷基，优选地R 1选自乙基、正丙基、异丙基、正丁基、异丁基、正戊基、异戊基、正己基、正辛基和2-乙基己基；
    -通式(I)、通式(I′)或通式(I″)中，R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基，优选地R 2和R 3各自独立为氢、甲基、乙基、氯甲基、氯乙基、溴甲基或溴乙基；
    -通式(II)中，R 5和R 7为氢或C 1～C 5的直链或支链的烷基，R 6为C 1～C 5的直链或支链的亚烷基；
    -所述卤素选自氯、溴和碘，优选为氯；
    -所述通式(II)所示的化合物是选自乙醇胺、二乙醇胺、三乙醇胺、N,N-二甲基乙醇胺、N,N-二乙基乙醇胺和N-甲基二乙醇胺中的一种或多种。
  4. 权利要求2所述的烯烃聚合催化剂载体，其特征在于，所述载体的平均颗粒直径为10-100微米，优选为30-70微米，并且所述载体的粒径分布小于1.2，优选为0.7-0.9。
  5. 权利要求1的烯烃聚合催化剂的载体，其包含通式(I″′)所示的组合物：
    Figure PCTCN2021126397-appb-100007
    通式(I″′)中，R 1为C 1～C 12的直链或支链的烷基；R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；X为卤素；m为0.1～1.9；n为0.1～1.9；m+n＝2；0<z<0.5；LB为通式(II)所示的酰胺类化合物，
    Figure PCTCN2021126397-appb-100008
    通式(II′)中，R 10为氢、氨基或C 1～C 8的直链或支链的烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基。
  6. 根据权利要求5所述的载体，其具有以下特征至少之一：
    -R 1为C 1～C 8的直链或支链的烷基，优选地R 1选自乙基、正丙基、异丙基、正丁基、异丁基、正戊基、异戊基、正己基、正辛基和2-乙基己基；
    -R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基，优选地R 2和R 3各自独立为甲基、乙基、氯甲基、氯乙基、溴甲基和溴乙基；
    -R 10为氢、氨基或C 1～C 5的直链或支链的烷基，R 11和R 12为氢或C 1～C 5的直链或支链的烷基；
    -所述卤素选自氯、溴和碘，优选为氯；
    -所述酰胺类化合物是选自甲酰胺、乙酰胺、丙酰胺、N-甲基乙酰胺、N,N-二甲基乙酰胺和碳酰胺中的一种或多种；
    -所述载体为球形，平均颗粒直径为10-100微米，优选为30-70微米，粒径分布小于1.2，优选为0.7-0.9。
  7. 根据权利要求5所述的载体，其还包含除镁以外的其他金属组分，优选地所述其他金属组分是铁和铜中的一种或两种；优选地所述其他金属组分在所述固体组分中的重量百分含量为0-1％。
  8. 一种用于制备烯烃聚合催化剂的载体的方法，该方法包括以下步骤：
    (a)将通式MgX 2所示的卤化镁、任选的金属卤化物、通式R 1OH所示的醇类化合物和通式(II)或(II′)所示的化合物反应形成溶液，
    Figure PCTCN2021126397-appb-100009
    其中，X为卤素；R 1为C 1～C 12的直链或支链的烷基；R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基；R 10为氢、氨基或C 1～C 8的直链或支链的烷基；R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基；
    (b)将步骤(a)形成的溶液与环氧化合物反应，直接生成球形固体颗粒；和
    (c)回收步骤(b)中形成的球形固体颗粒。
  9. 权利要求8所述的方法，其包括以下步骤：
    (a)将通式MgX 2所示的卤化镁、任选的结构式为FeY 2的金属卤化物或者任选的结构式为CuYc的金属卤化物与通式R 1OH所示的醇类化合物和通式(II)所示的化合物反应形成溶液，
    Figure PCTCN2021126397-appb-100010
    其中，R 1为C 1～C 12的直链或支链的烷基，R 5和R 7相同或不同，为氢或未取代或羟基取代的C 1～C 8的直链或支链的烷基；R 6为C 1～C 8的直链或支链的亚烷基，X和Y为卤素，c＝1或2；
    (b)将步骤(a)形成的溶液与环氧化合物反应，直接生成球形固体颗粒，优选地所述环氧化合物如通式(III)所示，
    Figure PCTCN2021126397-appb-100011
    其中，R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基；和
    (c)回收步骤(b)中形成的球形固体颗粒。
  10. 根据权利要求9所述的制备方法，其具有以下特征至少之一：
    -R 1为C 1～C 8的直链或支链的烷基，优选地R 1为C 1～C 6的直链或支链的烷基；
    -R 5和R 7为氢或C 1～C 5的直链或支链的烷基，R 6为C 1～C 5的直链或支链的亚烷基；
    -R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基。
    -步骤(a)中，在溶液的制备过程中加入高分子分散稳定剂，其重均分子量大于1000，优选大于3000，
    -卤化镁是选自二氯化镁、二溴化镁和二碘化镁中的一种或多种；
    -金属卤化物是选自氯化亚铁、四水合氯化亚铁、溴化亚铁和碘化亚铁中的一种或多种，优选氯化亚铁及其水合物；
    -所述载体的平均颗粒直径为10-100微米，优选为30-70微米；
    -所述载体的粒径分布小于1.2，优选为0.7-0.9；
    -所述步骤(a)中，所述溶液的制备在30-160℃温度下进行，优选40-120℃；
    -其中R 1OH化合物的加入量以每摩尔镁计为3-30摩尔，优选4-25摩尔；
    -通式(II)所示的化合物的加入量与所加入的卤化镁的摩尔比为1：100～1：5，优选1：50～1：5；
    -金属卤化物的加入量以每摩尔镁计为0.001-0.1摩尔，优选0.003-0.08；
    -所述步骤(b)中反应温度为30-160℃，优选40-120℃，
    -步骤(b)中环氧乙烷类化合物加入量以每摩尔镁计为1-10摩尔，优选2-6摩尔。
  11. 权利要求8所述的方法，其包括以下步骤：
    (a)将通式MgX 2所示的卤化镁与通式R 1OH所示的醇类化合物和通式(II′)所示的酰胺类化合物反应形成溶液，
    Figure PCTCN2021126397-appb-100012
    其中，R 1为C 1～C 12的直链或支链的烷基，R 10为氢、氨基或C 1～C 8的直链或支链的烷基，R 11和R 12相同或不同，为氢或C 1～C 8的直链或支链的烷基，X为卤素；
    (b)将步骤(a)形成的溶液与环氧化合物反应，直接生成固体组分，优选地所述环氧化合物如通式(III)所示，
    Figure PCTCN2021126397-appb-100013
    其中，R 2和R 3相同或不相同，为氢或未取代或卤素取代的C 1～C 5的直链或支链的烷基。
  12. 权利要求11所述的方法，其具有以下特征至少之一：
    -R 1为C 1～C 8的直链或支链的烷基；
    -R 10为氢、氨基或C 1～C 5的直链或支链的烷基，R 11和R 12为氢或C 1～C 5的直链或支链的烷基；
    -R 2和R 3各自独立为氢、C 1-C 3的直链或支链的烷基或卤素取代的C 1-C 3的直链或支链的烷基；
    -步骤(a)中，在溶液的制备过程中加入具有还原性的金属卤化物，优选地所述金属卤化物的通式为MY a，式中Y为卤素，M选自铜和铁中的一种或多种，a为1或2；更优选地，所述金属卤化物选自氯化亚铜和氯化亚铁；金属卤化物的加入量以每摩尔镁计为0.001-0.1摩尔，优选0.003-0.08；
    -步骤(a)中，在溶液的制备过程中加入高分子分散稳定剂，其重均分子量大于1000，优选大于3000；
    -所述步骤(a)中所述溶液的制备在30-160℃温度下进行，优选40-120℃；
    -步骤(a)中R 1OH化合物的加入量以每摩尔镁计为3-30摩尔，优选4-25摩尔；
    -通式(II′)所示的化合物的加入量与所加入的卤化镁的摩尔比为1：100～1：5，优选1：50～1：5；
    -所述步骤(b)中反应温度为30-160℃，优选40-120℃；
    -步骤(b)中环氧乙烷类化合物加入量以每摩尔镁计为1-10摩尔，优选2-6摩尔；
    -所述固体组分为球形，平均颗粒直径为10-100微米，优选为30-70微米，粒径分布小于1.2，优选为0.7-0.9。
  13. 一种用于烯烃聚合的催化剂组分，其含有由权利要求1-7中任一项所述的载体与钛化合物和内给电子体化合物的反应产物。
  14. 一种用于烯烃聚合的催化剂体系，其含有权利要求13所述的催化剂组分、烷基铝化合物以及任选的外给电子体化合物。
  15. 一种烯烃聚合方法，包括在烯烃聚合条件下，将一种或多种烯烃与权利要求14所述的催化剂体系接触以形成烯烃聚合物，和回收所得到的烯烃聚合物。
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CN109400778A (zh) 2017-08-18 2019-03-01 中国石油化工股份有限公司 用于烯烃聚合的催化剂组分及其制备方法和用于烯烃聚合的催化剂以及烯烃聚合方法
CN109400763A (zh) 2017-08-18 2019-03-01 中国石油化工股份有限公司 烯烃聚合催化剂载体及其制备方法和应用
CN111072803A (zh) 2018-10-19 2020-04-28 中国石油化工股份有限公司 烯烃聚合催化剂载体及其制备方法和应用
CN111072804A (zh) 2018-10-19 2020-04-28 中国石油化工股份有限公司 烯烃聚合催化剂组分及其应用和烯烃聚合催化剂及烯烃聚合方法
CN111072811A (zh) 2018-10-19 2020-04-28 中国石油化工股份有限公司 烯烃聚合催化剂球形载体及其制备方法和催化剂组分与催化剂及其应用

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