WO2009027266A1 - Catalyst for the polymerization of olefins - Google Patents
Catalyst for the polymerization of olefins Download PDFInfo
- Publication number
- WO2009027266A1 WO2009027266A1 PCT/EP2008/060830 EP2008060830W WO2009027266A1 WO 2009027266 A1 WO2009027266 A1 WO 2009027266A1 EP 2008060830 W EP2008060830 W EP 2008060830W WO 2009027266 A1 WO2009027266 A1 WO 2009027266A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- compound
- ethylene
- polymerization
- catalyst
- alkyl
- 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
-
- 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
- C08F110/02—Ethene
Definitions
- the catalysts of the invention are suitably used in (co)polymerization processes of ethylene to prepare (co)polymers having narrow Molecular Weight Distribution (MWD) and high activity.
- the MWD is an important characteristic of ethylene polymers in that it affects both the rheological behavior, and therefore the processability, and the final mechanical properties.
- polymers with narrow MWD are suitable for films and injection molding in that deformation and shrinkage problems in the manufactured article are minimized.
- the width of the molecular weight distribution for the ethylene polymers is generally expressed as melt flow ratio F/E, which is the ratio between the melt index measured by a load of 21.6 Kg (melt index F) and that measured with a load of 2.16 Kg (melt index E).
- the measurements of melt index are carried out according to ASTM D- 1238 and at 190 0 C. Relatively low values of the said ratio indicate relatively narrow molecular weight distribution.
- the catalyst comprises a solid catalyst component consisting of a titanium compound supported on magnesium chloride, an alkyl-Al compound and an electron donor compound (external donor) selected from monoethers of the formula ROR".
- an electron donor compound selected from monoethers of the formula ROR.
- Good results in terms of narrow MWD are only obtained when the solid component also contains an internal electron donor compound (diisobutylphthalate).
- the catalyst activity is unsatisfactory. This latter characteristic is very important in the operation of the plants because it assures competitiveness of the production plant. Hence, it would be highly desirable to have a catalyst capable to produce polymers with narrow molecular weight distribution, in high yields.
- JP 6-256413 discloses the copolymerization of ethylene with butene-1 in the presence of a catalyst comprising (A) a solid catalyst component supported on silica and comprising MgCl 2 , TiCb and an electron donor like tetrahydrofurane, (B) one or more aluminum alkyl compounds optionally halogenated and (C) a specific alkyl trialkoxysilane in which the alkyl is of formula -C(CH 3 ) 2 -CH(R2)(R3) where R2 and R3 are C1-C3 hydrocarbon groups.
- a catalyst comprising (A) a solid catalyst component supported on silica and comprising MgCl 2 , TiCb and an electron donor like tetrahydrofurane, (B) one or more aluminum alkyl compounds optionally halogenated and (C) a specific alkyl trialkoxysilane in which the alkyl is of formula -C(CH 3 ) 2 -CH(R2)(
- a novel catalyst for the (co)polymerization of ethylene comprising (A) a solid catalyst component comprising Ti, Mg, halogen, and optionally an electron donor compound in a donor/Ti molar ratio lower than 3, (B) an aluminum alkyl compound and (C) a silicon compound of formula RmSi(OEt)n in which R is C1-C20 alkyl group, m is an integer ranging from 1 to 3, n is (4-m) with the proviso that when R is equal to, or higher than C3, m is 1 or 2.
- a preferred subgroup of silicon compounds (C) is that in which R is C1-C4, preferably C1-C3 linear or branched alkyl, and m is 2.
- Preferred compounds are dimethyldiethoxysilane, diethyldiethoxysilane, di-isopropyldiethoxysilane di-n- butyldiethoxysilane.
- Another group of preferred silicon compound (C) are those in which R is branched alkyl having more than 3 carbon atoms, m is 1 and n is 3. Among them preferred compounds are isobutyltriethoxysilane, thexyltriethoxysilane. Cyclohexylmethyldiethoxysialne is also a usable compound.
- the silicon compound (C) is used in amounts such as to give a (B)/(C) molar ratio ranging from 0.1 to 100 preferably from 1 to 50 and more preferably from 5 to 30.
- the catalyst component of the invention comprises a Ti compound having at least one Ti-halogen bond supported on a magnesium chloride which is preferably magnesium dichloride and more preferably magnesium dichloride in active form.
- magnesium chloride means magnesium compounds having at least one magnesium chloride bond.
- the catalyst component may also contain groups different from halogen, in any case in amounts lower than 0.5 mole for each mole of titanium and preferably lower than 0.3.
- the catalysts of the invention preferably show a porosity Pp determined with the mercury method higher than 0.3 cm /g and more preferably higher than 0.5 usually in the range 0.5-0.8 cm 3 /g.
- the total porosity P ⁇ can be in the range of 0.50-1.50 cm 3 /g, particularly in the range of from 0.60 and 1.2 cm 3 /g, and the difference
- PT-PF can be higher than 0.1 preferably in the range from 0.15-0.50.
- the surface area measured by the BET method is preferably lower than 80 and in particular comprised between 10 and 70 m 2 /g.
- the porosity measured by the BET method is generally comprised between 0.1 and 0.5, preferably from 0.1 to 0.4 cm /g.
- the average pore radius value, for porosity due to pores up to 1 ⁇ m, is in the range from 600 to 1200 A.
- the particles of solid component have substantially spherical morphology and average diameter comprised between 5 and 150 ⁇ m, preferably from 20 to 100 ⁇ m and more preferably from 30 to 90 ⁇ m.
- particles having substantially spherical morphology those are meant wherein the ratio between the greater axis and the smaller axis is equal to or lower than 1.5 and preferably lower than 1.3.
- the solid the components of the invention may in principle comprise an electron donor compound (internal donor), selected for example among ethers, esters, amines and ketones.
- an electron donor compound selected for example among ethers, esters, amines and ketones.
- an electron donor compound only in amount such as to give ED/Ti ratios lower than 3, preferably lower than 1 and more preferably not to include any amount of electron donor compound in order for it to be absent in the final solid catalyst component (A).
- the preferred titanium compounds have the formula Ti(OR ⁇ ) n X y - n , wherein n is a number comprised between 0 and 0.5 inclusive, y is the valence of titanium, R ⁇ is an alkyl, cycloalkyl or aryl radical having 1 -8 carbon atoms and X is halogen.
- R can be ethyl, isopropyl, n-butyl, isobutyl, 2-ethylhexyl, n-octyl and phenyl, (benzyl);
- X is preferably chlorine. If y is 4, n varies preferably from O to 0.02; if y is 3, n varies preferably from 0 to 0.015. TiCU is especially preferred.
- a method suitable for the preparation of spherical components mentioned above comprises a first step (a) in which a compound MgCU.mR OH, wherein 0.3 ⁇ m ⁇ 1.7 and R is an alkyl, cycloalkyl or aryl radical having 1-12 carbon atoms is reacted with the said titanium compound of the formula Ti(OR ⁇ ) n X y _ n , in which n, y, X and R ⁇ have the same meaning defined above.
- MgCl2.mR m OH represents a precursor of Mg dihalide.
- These kind of compounds can generally be obtained by mixing alcohol and magnesium chloride in the presence of an inert hydrocarbon immiscible with the adduct, operating under stirring conditions at the melting temperature of the adduct (100-130 0 C). Then, the emulsion is quickly quenched, thereby causing the solidification of the adduct in form of spherical particles. Representative methods for the preparation of these spherical adducts are reported for example in USP 4,469,648, USP 4,399,054, and WO98/44009.
- Adducts having the desired final alcohol content can be obtained by directly using the selected amount of alcohol directly during the adduct preparation. However, if adducts with increased porosity are to be obtained it is convenient to first prepare adducts with more than 1.7 moles of alcohol per mole of MgCl 2 and then subjecting them to a thermal and/or chemical dealcoholation process. The thermal dealcoholation process is carried out in nitrogen flow at temperatures comprised between 50 and 15O 0 C until the alcohol content is reduced to the value ranging from 0.3 to 1.7. A process of this type is described in EP 395083.
- these dealcoholated adducts are also characterized by a porosity (measured by mercury method ) due to pores with radius due to pores with radius up to 0. l ⁇ m ranging from 0.15 to 2.5 cm /g preferably from 0.25 to 1.5 cm /g.
- the molar ratio Ti/Mg is stoichiometric or higher; preferably this ratio is higher than 3. Still more preferably a large excess of titanium compound is used.
- Preferred titanium compounds are titanium tetrahalides, in particular TiCU.
- the reaction with the Ti compound can be carried out by suspending the adduct in cold TiCU (generally 0 0 C); the mixture is heated up to 80-140 0 C and kept at this temperature for 0.5-8 preferably from 0.5 to 3 hours. The excess of titanium compound can be separated at high temperatures by filtration or sedimentation and siphoning.
- the catalyst component (B) of the invention is selected from Al-alkyl compounds possibly halogenated.
- it is selected from Al-trialkyl compounds, for example Al- trimethyl, Al-triethyl , Al-tri-n-butyl , Al-triisobutyl are preferred.
- the Al/Ti ratio is higher than 1 and is generally comprised between 5 and 800.
- the above-mentioned components (A)-(C) can be fed separately into the reactor where, under the polymerization conditions can exploit their activity. It may be advantageous to carry out a pre-contact of the above components, optionally in the presence of small amounts of olefins, for a period of time ranging from 0.1 to 120 minutes preferably in the range from 1 to 60 minutes.
- the pre-contact can be carried out in a liquid diluent at a temperature ranging from 0 to 90 0 C preferably in the range of 20 to 70 0 C.
- the so formed catalyst system can be used directly in the main polymerization process or alternatively, it can be pre -polymerized beforehand.
- a pre -polymerization step is usually preferred when the main polymerization process is carried out in the gas phase.
- the pre -polymerization step can be carried out at temperatures from 0 to 80 0 C, preferably from 5 to 70 0 C, in the liquid or gas phase.
- the pre-polymerization step can be performed in-line as a part of a continuous polymerization process or separately in a batch process.
- the batch pre-polymerization of the catalyst of the invention with ethylene in order to produce an amount of polymer ranging from 0.5 to 20 g per gram of catalyst component is particularly preferred.
- the pre -polymerized catalyst component can also be subject to a further treatment with a titanium compound before being used in the main polymerization step. In this case the use of TiCU is particularly preferred.
- the reaction with the Ti compound can be carried out by suspending the prepolymerized catalyst component in the liquid Ti compound optionally in mixture with a liquid diluent; the mixture is heated to 60-120 0 C and kept at this temperature for 0.5-2 hours.
- the catalysts of the invention can be used in any kind of polymerization process both in liquid and gas-phase processes. Catalysts having small particle size, (less than 40 ⁇ m) are particularly suited for slurry polymerization in an inert medium, which can be carried out continuously stirred tank reactor or in loop reactors. Catalysts having larger particle size are particularly suited for gas-phase polymerization processes which can be carried out in agitated or fluidized bed gas-phase reactors.
- the catalysts of the present invention are particularly suitable for preparing ethylene polymers having narrow molecular weight distribution that are characterized by a F/E ratio equal to, and preferably lower than, 30 in combination with a high polymerization activity.
- the catalysts of the present invention are also suitable for preparing very-low-density and ultra-low-density polyethylenes (VLDPE and ULDPE, having a density lower than 0.920g/cm 3 , to 0.880 g/cm ) consisting of copolymers of ethylene with one or more alpha-olefins having from 3 to 12 carbon atoms, having a mole content of units derived from ethylene of higher than
- the properties are determined according to the following methods:
- Melt index (M.I.) are measured at 190 0 C following ASTM D-1238 over a load of:
- a magnesium chloride and alcohol adduct containing about 3 mo Is of alcohol was prepared following the method described in example 2 of USP 4,399,054, but working at 2000 RPM instead of 10000 RPM.
- the adduct were subject to a thermal treatment, under nitrogen stream, over a temperature range of 50-150 0 C until a weight content of 25% of alcohol was reached.
- the pre -polymerized solid catalyst component (A) was employed in the ethylene polymerization according to the general procedure using the type and amount of silicon compound (C) reported in table 1 together with the polymerization results.
- CMDES Cyclohexylmethyldiethoxysilane
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- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2010522313A JP2010537026A (en) | 2007-08-29 | 2008-08-19 | Catalyst for olefin polymerization |
BRPI0816051-1A2A BRPI0816051A2 (en) | 2007-08-29 | 2008-08-19 | CATALYST FOR OLEFIN POLYMERIZATION |
EP08787312A EP2183288A1 (en) | 2007-08-29 | 2008-08-19 | Catalyst for the polymerization of olefins |
US12/733,340 US20100292420A1 (en) | 2007-08-29 | 2008-08-19 | Catalyst for the polymerization of olefins |
CN200880104574A CN101790545A (en) | 2007-08-29 | 2008-08-19 | catalyst for the polymerization of olefins |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP07115168.2 | 2007-08-29 | ||
EP07115168 | 2007-08-29 | ||
US99327107P | 2007-09-11 | 2007-09-11 | |
US60/993,271 | 2007-09-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2009027266A1 true WO2009027266A1 (en) | 2009-03-05 |
Family
ID=39766606
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2008/060830 WO2009027266A1 (en) | 2007-08-29 | 2008-08-19 | Catalyst for the polymerization of olefins |
Country Status (6)
Country | Link |
---|---|
US (1) | US20100292420A1 (en) |
EP (1) | EP2183288A1 (en) |
JP (1) | JP2010537026A (en) |
CN (1) | CN101790545A (en) |
BR (1) | BRPI0816051A2 (en) |
WO (1) | WO2009027266A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2602269A1 (en) | 2011-12-06 | 2013-06-12 | Basell Polyolefine GmbH | Multistage process for the polymerization of olefins |
EP2803680A1 (en) | 2013-05-16 | 2014-11-19 | Basell Polyolefine GmbH | Multistage process for the polymerization of olefins |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2287212B1 (en) | 2009-08-21 | 2014-03-26 | China Petroleum & Chemical Corporation | A catalyst component for ethylene polymerization, preparation thereof and a catalyst comprising the catalyst component |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2512033A1 (en) * | 1981-08-25 | 1983-03-04 | Nippon Oil Co Ltd | PROCESS FOR THE PRODUCTION OF POLY-OLEFINS |
FR2541291A1 (en) * | 1982-12-27 | 1984-08-24 | Nippon Oil Co Ltd | CATALYTIC PROCESS FOR THE PREPARATION OF POLYOLEFINS |
EP0578470A2 (en) * | 1992-07-06 | 1994-01-12 | Nippon Oil Co. Ltd. | Process for preparing polyolefins |
WO1994006833A1 (en) * | 1992-09-14 | 1994-03-31 | Shell Oil Company | Process for polymerizing alpha-olefin |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
IT1096661B (en) * | 1978-06-13 | 1985-08-26 | Montedison Spa | PROCEDURE FOR THE PREPARATION OF SOLID SPHEROIDAL PRODUCTS AT AMBIENT TEMPERATURE |
IT1098272B (en) * | 1978-08-22 | 1985-09-07 | Montedison Spa | COMPONENTS, CATALYSTS AND CATALYSTS FOR THE POLYMERIZATION OF ALPHA-OLEFINS |
US4451688A (en) * | 1981-12-03 | 1984-05-29 | Nippon Oil Company, Limited | Process for preparing polyolefins |
FI80055C (en) * | 1986-06-09 | 1990-04-10 | Neste Oy | Process for preparing catalytic components for polymerization of olefins |
FR2640273B1 (en) * | 1988-12-14 | 1992-09-04 | Atochem | PROCESS FOR THE GAS PHASE POLYMERIZATION OF ETHYLENE ALLOWING THE MANUFACTURE OF NARROW MOLECULAR MASS DISTRIBUTION POLYETHYLENE |
JP2879347B2 (en) * | 1989-10-02 | 1999-04-05 | チッソ株式会社 | Manufacturing method of olefin polymerization catalyst |
US6818583B1 (en) * | 1999-04-15 | 2004-11-16 | Basell Poliolefine Italia S.P.A. | Components and catalysts for the polymerization of olefins |
IL141358A0 (en) * | 1999-06-18 | 2002-03-10 | Basell Technology Co Bv | Catalyst components for the polymerization of olefins and catalysts obtained therefrom |
-
2008
- 2008-08-19 JP JP2010522313A patent/JP2010537026A/en not_active Withdrawn
- 2008-08-19 US US12/733,340 patent/US20100292420A1/en not_active Abandoned
- 2008-08-19 BR BRPI0816051-1A2A patent/BRPI0816051A2/en not_active Application Discontinuation
- 2008-08-19 EP EP08787312A patent/EP2183288A1/en not_active Withdrawn
- 2008-08-19 CN CN200880104574A patent/CN101790545A/en active Pending
- 2008-08-19 WO PCT/EP2008/060830 patent/WO2009027266A1/en active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2512033A1 (en) * | 1981-08-25 | 1983-03-04 | Nippon Oil Co Ltd | PROCESS FOR THE PRODUCTION OF POLY-OLEFINS |
FR2541291A1 (en) * | 1982-12-27 | 1984-08-24 | Nippon Oil Co Ltd | CATALYTIC PROCESS FOR THE PREPARATION OF POLYOLEFINS |
EP0578470A2 (en) * | 1992-07-06 | 1994-01-12 | Nippon Oil Co. Ltd. | Process for preparing polyolefins |
WO1994006833A1 (en) * | 1992-09-14 | 1994-03-31 | Shell Oil Company | Process for polymerizing alpha-olefin |
Non-Patent Citations (1)
Title |
---|
See also references of EP2183288A1 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2602269A1 (en) | 2011-12-06 | 2013-06-12 | Basell Polyolefine GmbH | Multistage process for the polymerization of olefins |
WO2013083548A2 (en) | 2011-12-06 | 2013-06-13 | Basell Polyolefine Gmbh | Multistage process for the polymerization of olefins |
EP2803680A1 (en) | 2013-05-16 | 2014-11-19 | Basell Polyolefine GmbH | Multistage process for the polymerization of olefins |
Also Published As
Publication number | Publication date |
---|---|
US20100292420A1 (en) | 2010-11-18 |
JP2010537026A (en) | 2010-12-02 |
BRPI0816051A2 (en) | 2015-03-03 |
EP2183288A1 (en) | 2010-05-12 |
CN101790545A (en) | 2010-07-28 |
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