WO2002026838A1 - Catalyseur supporte sur gel de silice se pretant a la polymerisation ou a la copolymerisation ethylenique - Google Patents
Catalyseur supporte sur gel de silice se pretant a la polymerisation ou a la copolymerisation ethylenique Download PDFInfo
- Publication number
- WO2002026838A1 WO2002026838A1 PCT/CN2001/001264 CN0101264W WO0226838A1 WO 2002026838 A1 WO2002026838 A1 WO 2002026838A1 CN 0101264 W CN0101264 W CN 0101264W WO 0226838 A1 WO0226838 A1 WO 0226838A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- titanium
- catalyst component
- polymerization
- catalyst
- supported catalyst
- Prior art date
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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
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F10/02—Ethene
-
- 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
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
- Y10S526/901—Monomer polymerized in vapor state in presence of transition metal containing catalyst
Definitions
- the invention relates to a silica gel-supported catalyst component suitable for ethylene polymerization or copolymerization, a catalyst, and an application thereof in ethylene polymerization or copolymerization, in particular, its application in the condensation operation of a gas-phase fluidized bed.
- micro-spherical silica gel (average particle size of 10 to 100 ⁇ m) has been widely used as a carrier in olefin polymerization catalysts, especially in catalysts for gas phase olefin polymerization.
- a large number of silica gels have been used by the American company GRACE.
- SYLOPOL948, SYLOPOL955, XPO-2402, and SD490 of CROSFIELD the specific surface area of these silica gels is generally ⁇ 300m 2 / g, and some are even lower, so when they are applied to supported catalysts, the load of active components is limited , Which affects the improvement of catalyst activity.
- US4303771 discloses a series of catalysts suitable for gas-phase fluidized-bed ethylene polymerization processes using the above-mentioned types of silica gel as a carrier.
- catalysts that have been widely commercialized are mostly magnesium Compounds, titanium compounds, and electron donor compounds are supported on SYLOPOL 955 silica gel.
- the activity of ethylene polymerization on industrial gas-phase fluidized-bed devices is generally ⁇ 3500 gPE / g Cat, but when used in gas-phase fluidized-bed condensation technology, Due to the shortened catalyst residence time, the activity is significantly reduced, resulting in an increase in the ash content of the ethylene polymer and affecting the quality of the ethylene polymer. Therefore, improving the activity of such catalysts is one of the key factors to improve the quality of ethylene polymers.
- the silica gel carrier currently used in commercial fumed polyethylene generally controls the specific surface area to be ⁇ 300m 2 / g.
- a catalyst formed by supporting a magnesium compound, a titanium compound, and an electron donor compound, and also a halogenated modifier is used in the polymerization of olefins. Not only has the activity of the catalyst been greatly improved, but also the hydrogen regulation sensitivity of the catalyst and the copolymerization performance of olefins have been significantly improved. It has shown good comprehensive performance when used in the currently advanced gas-phase fluidized bed condensation technology.
- the purpose of the present invention is to overcome the shortcomings of the low activity of the titanium-based catalyst using silica gel as a support in the prior art, and to propose a highly active silica-supported catalyst component for ethylene polymerization or copolymerization.
- a second object of the present invention is to provide a catalyst for the polymerization or copolymerization of ethylene.
- a third object of the present invention is to provide an application of the above catalyst in olefin polymerization or copolymerization.
- a highly active silica-supported catalyst component for ethylene polymerization or copolymerization which is a titanium-containing active component supported on a porous inert carrier material, and the titanium-containing activity
- the component is a reaction product including at least one titanium compound, at least one substitution improver, at least one magnesium compound, and at least one electron donor,
- the porous carrier material is a spherical or spheroidal silica gel with an average particle diameter of 10 to 100 ⁇ m, a specific surface area of 300 to 1000 m 2 / g, a pore volume of 2.0 to 5.0 ml / g, and an average pore diameter of 5 to 45mn.
- a catalyst comprising the supported catalyst component of the present invention.
- a third aspect of the present invention there is provided an application of the catalyst of the present invention in the polymerization or copolymerization of a fluorene.
- a reaction product of at least one titanium compound, at least one magnesium compound, and at least one electron donor is supported on a support by an impregnation method.
- the support material is selected from a Spherical or quasi-spherical silica gel with a large specific surface area is preferably dehydrated silica gel.
- the content of hydroxyl groups on the surface of the silica gel can be adjusted by controlling the thermal activation conditions of the silica gel.
- the average particle diameter of the silica gel is 10 to 100 ⁇ m, preferably 20 - 80 ⁇ , and most preferably 30 ⁇ 60 ⁇ ; specific surface area of 300 ⁇ 1000m 2 / g, preferably from 400 ⁇ 800m 2 / g, most preferably 600 ⁇ 800m 2 / g; pore volume of 1.0 ⁇ 6.0ml / g, preferably It is 2.0 ⁇ 5.0ml / g; the average diameter of pores is 5 ⁇ 45, preferably 10 ⁇ 35 tons.
- At least one kind of substitute modifier is also added, and the halogen modifier improves the formula A class of compounds, where F is a functional group that can chemically react with organoaluminum compounds, titanium compounds, or hydroxyl groups on silica gel, such as aldehyde, acyl, hydroxyl, amino, or ester groups; R 1 is a divalent d ⁇ C 6 aliphatic or aromatic group, which is connected to the functional group F; R 2 is hydrogen, unsubstituted or halogen substituted ( ⁇ ⁇ ( 6 alkyl, 0: 3 ⁇ ( 6 cycloalkyl or C 6 ⁇ C 10 aromatic group, b is 0, 1 or 2, X ⁇ F, C1 or Br.
- F is a functional group that can chemically react with organoaluminum compounds, titanium compounds, or hydroxyl groups on silica gel, such as aldehyde, acyl, hydroxyl, amino, or ester groups
- R 1 is a divalent d ⁇
- the modifier is a class of halogenated alcohols, and the specific compounds are 2, 2, 2-trichloroethanol (Cl 3 CCH 2 OH), 2, 2-dichloroethanol (Cl 2 CHCH 2 OH), 2-chloroethanol (ClCH 2 CH 2 OH), 1, 1-dimethyl-2, 2, 2-trichloroethanol (Cl 3 CC (CH 3 ) 2 OH), 4-chlorobutanol (ClCH 2 CH 2 CH 2 CH 2 OH), p-chlorophenol, m-chlorophenol, o-chlorophenol and 2-chlorocyclohexanol.
- the specific compounds are 2, 2, 2-trichloroethanol (Cl 3 CCH 2 OH), 2, 2-dichloroethanol (Cl 2 CHCH 2 OH), 2-chloroethanol (ClCH 2 CH 2 OH), 1, 1-dimethyl-2, 2, 2-trichloroethanol (Cl 3 CC (CH 3 ) 2 OH), 4-chlorobutanol (ClCH 2
- F is an acyl group
- the modifier is a type of haloacyl halide, and the specific compounds are trichloroacetyl chloride, dichloroacetyl chloride, chloroacetyl chloride, o-chlorobenzoyl chloride, 2-chlorocyclohexylcarbonyl chloride, and the like. Trichloroacetyl chloride, dichloroacetyl chloride or chloroacetyl chloride is preferred.
- the ratio between each component is calculated as per mole of the titanium compound as follows: the hafnium compound is 0.5 to 50 moles, preferably 1.5 to 5 moles, and the electron donor is 0.5 to 50 The mole is preferably 1 to 10 moles, and the substitute modifier is 0.5 to 50 moles, preferably 1 to 10 moles.
- the titanium compound used is preferably of formula 11 (011) 11 ⁇ 1 _ 4 or TiX, those represented by the formula wherein R 3 is Ci ⁇ C 14 aliphatic hydrocarbon group, X from F , Cl, Br or a mixture thereof, and n is an integer of 1 to 4.
- titanium tetrachloride titanium tetrabromide, titanium tetraiodide, tetrabutoxy titanium, tetraethoxy titanium, monochlorotriethoxy titanium, dichlorodiethoxy titanium, trichloromonoethyl
- titanium oxytitanium and hafnium trichloride or a mixture thereof is preferably titanium tetrachloride, titanium trichloromonoethoxylate, titanium trichloride, or the like.
- the magnesium compounds used therein are those represented by the general formula MgX 2 , where X is selected from Cl, Br, I or a mixture thereof. Specifically, magnesium dichloride, magnesium dibromide, and magnesium diiodide can be selected, and magnesium dichloride is preferred.
- the electron donor (ED) used therein is preferably selected from the following compounds: alkyl esters of aliphatic or aromatic carboxylic acids, aliphatic ethers, cyclic ethers, and aliphatic ketones.
- alkyl esters of d to C 4 saturated aliphatic carboxylic acids alkyl esters of C 7 to C 8 aromatic carboxylic acids, C 2 to C 6 aliphatic ethers, and C 3 to C 4 rings are preferred.
- Ether, C 3 ⁇ C 6 saturated aliphatic ketone alkyl esters of aliphatic or aromatic carboxylic acids, aliphatic ethers, cyclic ethers, and aliphatic ketones.
- the electron donor can be used alone or in combination.
- the catalyst component of the present invention is prepared by dissolving the above-mentioned titanium compound and magnesium compound in an electron donor to prepare a mother liquid, and then supporting the large specific surface area silica gel carrier by an impregnation method. The method preferably includes the following steps. :
- Activate the silica gel carrier by a conventional method. More preferred conditions can be dehydration at 600 ° C for 4 hours;
- step (2) Add the activated carrier in step (2) to the above mother liquor, and after a certain period of time, dry it, remove the excess solvent, ie, the electron donor, and generally control the remaining content to 10 ⁇ 21wt%;
- step (4) Suspend the solid material obtained in step (4) in a lower alkane solvent, perform reduction treatment with one or more alkyl aluminum compounds, and then dry to obtain the final catalyst component.
- the lower alkane solvents mentioned in step (2) and step (5) are C 3 ⁇ C 9 alkanes, preferably C 5 and C 6 alkanes, such as isopentane, pentamidine, hexane and the like;
- the aluminum alkyl compound of step (2) and step (5) is preferably used in the general formula AlR m 'X 3 _ those represented by the formula R ra' are the same or different d_ 8 alkyl group, X is Halogen, m is an integer from 1 to 3.
- Preferred aluminum alkyl compounds are AlEt 3 , Al (nC 6 H 13 ) 3 , AlEt 2 Cl, and the like.
- the halide improver of the present invention can be incorporated into the catalyst component in any effective manner.
- any of the following methods can be used to obtain a good promotion effect: i) introduced in the above silica gel treatment step (2), ii) introduced in step (4) of the above catalyst complex supported on silica , Iii) introduced in the catalyst reduction step (5) and the like.
- the invention also relates to a catalyst for the polymerization or copolymerization of ethylene, which is a reaction product of the titanium-containing catalyst component and an alkyl aluminum compound, wherein the alkyl aluminum compound used has the general formula A1R " 3 , wherein R "is identical or different alkyl d_ 8, wherein the one or two alkyl groups may be substituted with chlorine, an alkylaluminum can use a mixture of two or more, preferably AlEt 3, Al (iso- Bu) 3 , Al (nC 6 H 13 ) 3 , Al (nC 8 H 17 ) 3 , AlEt 2 Cl, and the like.
- the catalyst of the present invention is suitable for homopolymerization of various ethylene or copolymerization of ethylene with other ⁇ -olefins, in which ⁇ -olefins are propylene, butene, pentene, hexene, octene, 4-methylpentene-1 One of them.
- Its polymerization process can adopt gas phase method, slurry method and solution method, which is more suitable for gas phase fluidized bed polymerization, especially the condensation technology of gas phase fluidized bed.
- the polymerization temperature can be 50-100 ° C.
- the invention adopts a large specific surface area silica gel carrier, which obviously increases the titanium content of the active component of the catalyst on the premise of ensuring good particle performance of the catalyst, provides a base for improving the activity of the catalyst, and also has functional groups.
- the halide improver is fixed on the surface of silica gel through chemical reaction.
- step (2) The silica gel treated in step (2) is mixed with the mother liquor prepared in step (3), stirred at reflux for 1 hour, and then purged and dried with high-purity nitrogen to obtain a fluid light yellow solid powder, of which tetrahydrofuran The content was 16.0 wt%.
- step ( 5 ) using isopentane as a solvent at room temperature, pre-reducing the reaction product obtained in step (4) with AlEt 2 Cl and Al (nC 6 H 13 ) 3 , and controlling the molar ratio of AlEt 2 Cl / THF to 0.45, Al (nC 6 Hi 3 ) 3 / THF was 0.20, and 100 ml of hexane was added.
- 7.2 ml of a solution of AlEt 2 Cl in hexane (2.21 mmol) was added dropwise, and the reaction was completed for half an hour after the dropwise addition.
- Step (4) 111% of the obtained powder is 15.7wt%
- Example 3 The catalyst slurry polymerization was evaluated in the same manner as in Example 1, and the polymerization results are shown in Table 1.
- Step (4) 1% by weight in the obtained powder is 17.7wt%
- Example 4 The catalyst slurry polymerization was evaluated in the same manner as in Example 1, and the polymerization results are shown in Table 1.
- Example 4 The catalyst slurry polymerization was evaluated in the same manner as in Example 1, and the polymerization results are shown in Table 1.
- the titanium content in the catalyst is 1.26wt%
- SYLOPOL 948 (produced by Grace, USA, with an average particle size of 50 ⁇ m, a specific surface area of 295 m 2 / g, a pore volume of 1.7 ml / g, and an average pore diameter of 23.3 mn).
- Silica gel is used in place of the silica gel used in Example 1. Change, do not use Cl 3 CC3 ⁇ 4OH when processing silica gel.
- Step (4) 1 « ⁇ % in the obtained powder is 13.5 wt%
- the titanium content in the catalyst is 0.9wt%
- the surface area of the catalyst component was 230 m 2 / g, and the pore volume was 1.8 ml / g, as measured by the mercury pressure method (apparatus: AUTOPORE 9410, MICROMERITICS, USA).
- SYLOPOL 948 silica gel is used instead of the silica gel used in Example 1, and the dosage is unchanged. Cl 3 CCH 2 OH is not used when processing the silica gel.
- Example 5 The catalyst slurry polymerization evaluation was the same as in Example 1. The polymerization results are shown in Table 1. Example 5
- the catalyst slurry polymerization evaluation was the same as in Example 1.
- the polymerization results are shown in Table 1.
- Step (4) 1% by weight in the obtained powder is 14.2% by weight
- the catalyst slurry polymerization was evaluated in the same manner as in Example 1, and the polymerization results are shown in Table 1.
- Example 1 1.26 6667 52.9 0.35 0.53 15.92 30.0 89.8 9.6 0.4 0.01 0.06 0.05 0.04 0.06 0.2
- Example 2 1.29 6160 47.8 0.34 053 16.44 31.0 86.1 10.6 1.4 0.5 0.3 0.4 0.4 0.3 1.4
- Example 3 1.14 4955 43.5 0.37 0.52 17.20 33.1 74.9 20.9 2.3 0.7 0.4 0.6 0.4 0.3 1.7
- Example 4 1.07 4649 43.4 0.38 0.52 15.30 29.4 61.3 28.9 4.0 1.6 1.0 1.3 1.2 0.7 4.2
- Example 5 1.26 6450 51.2 0.32 0.55 16.0 29.1 85.3 12.9 1.0 0.2 0.2 0.2 0.2 0.2 0.8
- Example 6 1.10 2800 25.5 0.35 0.26 7.9 30.4 63.8 32.1 22 0.5 0.4 0.4 0.4 0.2 1.4 Comparative Example 1 1.36 3946 29.0 0.32 0.18 5.41 30.1 73.5
- Example 1 3950 0.33 7.5 225.3 29.96 0.9247 57.6 38.2 3.2 0.5 0.3 0.2 0.0 0.0 0.5
- Example 5 5910 0.30 8.6 254.0 29.46 0.9281 57.3 33.9 5.4 1.6 0.9 0.6 0.3 0.0 1.8
- Example 6 6160 0.31 1.4 41.54 29.89 0.9309 73.1 22.6 2.9 0.8 0.3 0.2 0.1 0.0 0.6
- the present invention introduces an improver Cl 3 CCH 2 OH or Cl 3 CCOCl in the catalyst preparation process.
- the experimental results show that the activity of the catalyst is greatly improved while the polyethylene M1 is kept unchanged.
- the comparison between Example 1 and Comparative Example 3 shows that the catalyst activity is increased from 1200 gPE / g cat to 6667 gPE / g cat, while the MI remains basically unchanged.
- Example 2 and Comparative Example 3 From the comparison between Example 2 and Comparative Example 3, it is seen that the catalyst activity is 1200 g PE / g cat was increased to 6160 gPE / g cat, while MI remained basically unchanged; using Cl 3 CCH 2 OH as an improver, it is seen from the comparison between Example 3 and Comparative Example 4 that the catalyst activity is improved from 1160 g PE / g cat To 4955 gPE / g cat, while the MI remained unchanged; using Cl 3 CCOCl as an improver, it can be seen from the comparison between Example 4 and Comparative Example 4 that the catalyst activity increased from 1160 g PE / g cat to 4649 gPE / g cat, The MI remains unchanged.
- the catalysts according to the present invention not only have high activity, but also have good hydrogen regulation sensitivity, and are suitable for use in the gas phase method.
- slurry process ethylene homopolymerization or copolymerization process, especially suitable for condensed operation of gas-phase fluidized bed, high catalyst activity, low ash content of PE, conducive to low-cost, high-quality production of PE resins of various brands, It is especially suitable for producing various grades of LLDPE resin.
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- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2002213766A AU2002213766A1 (en) | 2000-08-22 | 2001-08-22 | Supported catalyst component suitable for ethylene (co)polymerization, a catalyst therefrom and use of the same |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN00123560.5 | 2000-08-22 | ||
CNB001235605A CN1181105C (zh) | 2000-08-22 | 2000-08-22 | 用于乙烯聚合或共聚合的高活性硅胶载体催化剂组分及其催化剂和该催化剂的应用 |
Publications (1)
Publication Number | Publication Date |
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WO2002026838A1 true WO2002026838A1 (fr) | 2002-04-04 |
Family
ID=4589962
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN2001/001264 WO2002026838A1 (fr) | 2000-08-22 | 2001-08-22 | Catalyseur supporte sur gel de silice se pretant a la polymerisation ou a la copolymerisation ethylenique |
Country Status (4)
Country | Link |
---|---|
US (1) | US6642325B2 (zh) |
CN (1) | CN1181105C (zh) |
AU (1) | AU2002213766A1 (zh) |
WO (1) | WO2002026838A1 (zh) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10163179A1 (de) * | 2001-12-21 | 2003-07-10 | Degussa | Granulate auf Basis von pyrogen hergestelltem Siliziumdioxid, Verfahren zu ihrer Herstellung und ihre Verwendung |
JP2006523730A (ja) * | 2003-02-24 | 2006-10-19 | ゾンクォーシーヨーファークォングーフェンヨーシェングォンス | プロピレン重合用触媒の複合担体、これを含む触媒成分及び触媒 |
US20060223693A1 (en) * | 2003-04-07 | 2006-10-05 | Kenichiro Fujimoto | Catalyst for producing hydrocarbon from synthsis gas and method for producing catalyst |
CN101235110B (zh) * | 2008-01-14 | 2010-12-08 | 中国石油天然气股份有限公司大庆化工研究中心 | 乙烯气相聚合或共聚合催化剂组合物及其制备方法 |
CN102040687B (zh) * | 2009-10-20 | 2013-09-25 | 中国石油化工股份有限公司 | 一种用于乙烯聚合反应的催化剂组分及其催化剂 |
US9156922B2 (en) * | 2010-03-04 | 2015-10-13 | Total Research & Technology Feluy | Modified catalyst supports |
CA2760264C (en) | 2011-12-05 | 2018-08-21 | Nova Chemicals Corporation | Passivated supports for use with olefin polymerization catalysts |
CN102585055B (zh) * | 2012-02-17 | 2013-12-18 | 中国石油化工股份有限公司 | 一种烯烃聚合催化剂、制备方法和应用 |
EP3018150B1 (en) | 2014-11-07 | 2020-03-11 | Indian Oil Corporation Limited | Process for the preparation of spherical catalyst particles |
CN111040057B (zh) * | 2018-10-15 | 2023-01-03 | 中国石油化工股份有限公司 | 一种烯烃聚合反应催化剂、制备方法及复合催化剂 |
Citations (6)
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US4242231A (en) * | 1978-04-12 | 1980-12-30 | Toa Nenryo Kogyo Kabushiki Kaisha | Catalyst component for use in the polymerization of α-olefins and a method of using the same |
US4242230A (en) * | 1978-04-12 | 1980-12-30 | Toa Nenryo Kogyo Kabushiki Kaisha | Catalyst component for use in the polymerization of α-olefins and a method of using the same |
US5661097A (en) * | 1994-08-12 | 1997-08-26 | The Dow Chemical Company | Supported olefin polymerization catalyst |
EP0812861A1 (de) * | 1996-06-11 | 1997-12-17 | BASF Aktiengesellschaft | Katalysatorsysteme vom Typ der Ziegler-Natta-Katalysatoren |
US5744567A (en) * | 1995-12-06 | 1998-04-28 | Basf Aktiengesellschaft | Random propylene copolymers |
CN1230552A (zh) * | 1998-03-11 | 1999-10-06 | 住友化学工业株式会社 | 固体催化剂组份和用于烯烃聚合的催化剂,以及制备烯烃聚合物的方法 |
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US3225023A (en) | 1962-11-30 | 1965-12-21 | Phillips Petroleum Co | Process for controlling melt index |
US4302566A (en) | 1978-03-31 | 1981-11-24 | Union Carbide Corporation | Preparation of ethylene copolymers in fluid bed reactor |
US4302565A (en) | 1978-03-31 | 1981-11-24 | Union Carbide Corporation | Impregnated polymerization catalyst, process for preparing, and use for ethylene copolymerization |
US4303771A (en) | 1978-12-14 | 1981-12-01 | Union Carbide Corporation | Process for the preparation of high density ethylene polymers in fluid bed reactor |
US4293673A (en) | 1978-12-28 | 1981-10-06 | Union Carbide Corporation | Spheroidal polymerization catalyst, process for preparing, and use for ethylene polymerization |
JPS5975910A (ja) * | 1982-10-25 | 1984-04-28 | Mitsui Petrochem Ind Ltd | エチレン共重合体 |
JPH0721018B2 (ja) * | 1985-07-05 | 1995-03-08 | 東燃料株式会社 | オレフイン重合用触媒成分の製造方法 |
US5079204A (en) * | 1990-04-30 | 1992-01-07 | Phillips Petroleum Company | Polymerization catalyst, preparation, and use |
-
2000
- 2000-08-22 CN CNB001235605A patent/CN1181105C/zh not_active Expired - Lifetime
-
2001
- 2001-08-22 WO PCT/CN2001/001264 patent/WO2002026838A1/zh active Application Filing
- 2001-08-22 US US09/935,333 patent/US6642325B2/en not_active Expired - Fee Related
- 2001-08-22 AU AU2002213766A patent/AU2002213766A1/en not_active Abandoned
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4242231A (en) * | 1978-04-12 | 1980-12-30 | Toa Nenryo Kogyo Kabushiki Kaisha | Catalyst component for use in the polymerization of α-olefins and a method of using the same |
US4242230A (en) * | 1978-04-12 | 1980-12-30 | Toa Nenryo Kogyo Kabushiki Kaisha | Catalyst component for use in the polymerization of α-olefins and a method of using the same |
US5661097A (en) * | 1994-08-12 | 1997-08-26 | The Dow Chemical Company | Supported olefin polymerization catalyst |
US5744567A (en) * | 1995-12-06 | 1998-04-28 | Basf Aktiengesellschaft | Random propylene copolymers |
EP0812861A1 (de) * | 1996-06-11 | 1997-12-17 | BASF Aktiengesellschaft | Katalysatorsysteme vom Typ der Ziegler-Natta-Katalysatoren |
CN1230552A (zh) * | 1998-03-11 | 1999-10-06 | 住友化学工业株式会社 | 固体催化剂组份和用于烯烃聚合的催化剂,以及制备烯烃聚合物的方法 |
Also Published As
Publication number | Publication date |
---|---|
AU2002213766A1 (en) | 2002-04-08 |
US20020065378A1 (en) | 2002-05-30 |
CN1181105C (zh) | 2004-12-22 |
CN1339509A (zh) | 2002-03-13 |
US6642325B2 (en) | 2003-11-04 |
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