CA1095494A - High efficiency catalyst for high bulk density polyethylene - Google Patents
High efficiency catalyst for high bulk density polyethyleneInfo
- Publication number
- CA1095494A CA1095494A CA287,774A CA287774A CA1095494A CA 1095494 A CA1095494 A CA 1095494A CA 287774 A CA287774 A CA 287774A CA 1095494 A CA1095494 A CA 1095494A
- Authority
- CA
- Canada
- Prior art keywords
- support
- titanium
- catalyst
- magnesium oxide
- methanol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
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
Abstract
ABSTRACT OF THE DISCLOSURE A unique high efficiency catalyst for the polymerization of ethylene has been developed based on the use of methanol treated magnesium oxide as support, an equimolar mixture of titanium tetrachloride and tetra-butyltitanate as titanium source impregnated on the support, and an organoaluminum compound as reducing agent. The polyethylene produced by this catalyst has narrow molecular weight distribution, high bulk density , high melt index, and minimum catalyst residue due to the high polymer to catalyst ratio.
Description
1~ 94 BACKGROUND OF THE INVENTION
The present invention relates to the polymeriza-tion of ethylene in the presence of supported catalysts known in the art as Ziegler catalysts.
Ziegler catalysts are commonly formed by reducing a transition metal compound with an organometallic compound.
The reduced transition metal compound is then used, in conjunction with an activator, which may be the same or a ; different organometallic compound, to polymerize olefins, especially ethylene, in the presence of an inert solvent or in the gas phase. A molecular weight regulator, such as hydrogen, may be used with these catalyst systems, as taught by Vandenberg in U.S. 3,051,690.
Such catalysts are often rather unefficient because the catalyst particles tend to agglomerate. To obviate this problem many systems of supporting the catalyst on solid carriers have been proposed.
Kashiwa et al, in U.S. 3,642,746, describe ~; cataly~ts utilizing a magnesium chloride support pretreatedwith an electron donor, such as methanol, and then treated with a titanium compound. The electron donor must be coordinated with the magnesium chloride when the titanium compound is added to the support.
Diedrich et al, in U.S. 3,644,318, describe catalysts supported on magnesium alcoholates.
Stevens et al, in U.S. 3,718,636 describes catalysts obtained by reacting a magnesium oxide support with an organometallic compound, separating the resulting solid product and reacting this product with a titanium compound. The polyethylene produced with this catalyst had low melt index and broad molecular weight dlstribution.
The present invention relates to the polymeriza-tion of ethylene in the presence of supported catalysts known in the art as Ziegler catalysts.
Ziegler catalysts are commonly formed by reducing a transition metal compound with an organometallic compound.
The reduced transition metal compound is then used, in conjunction with an activator, which may be the same or a ; different organometallic compound, to polymerize olefins, especially ethylene, in the presence of an inert solvent or in the gas phase. A molecular weight regulator, such as hydrogen, may be used with these catalyst systems, as taught by Vandenberg in U.S. 3,051,690.
Such catalysts are often rather unefficient because the catalyst particles tend to agglomerate. To obviate this problem many systems of supporting the catalyst on solid carriers have been proposed.
Kashiwa et al, in U.S. 3,642,746, describe ~; cataly~ts utilizing a magnesium chloride support pretreatedwith an electron donor, such as methanol, and then treated with a titanium compound. The electron donor must be coordinated with the magnesium chloride when the titanium compound is added to the support.
Diedrich et al, in U.S. 3,644,318, describe catalysts supported on magnesium alcoholates.
Stevens et al, in U.S. 3,718,636 describes catalysts obtained by reacting a magnesium oxide support with an organometallic compound, separating the resulting solid product and reacting this product with a titanium compound. The polyethylene produced with this catalyst had low melt index and broad molecular weight dlstribution.
2 ~
. ~
l~SL~]L94 BRIEF SUMMARY OF THE IN~rENTION
It has now been found that a catalyst having high efficiency for polymerizing ethylene is obtained by treating magnesium oxide with methanol, drylng the oxide free of alcohol, impregnating the oxide with a mixture of titanium tetrachloride and tetrabutyltitanate (1:1 mole ratio) and adding an alkylaluminum compound to reduce the titanium mixture. The polyethylene made with this catalyst has melt indices in the injection molding range, i.e. between 3.1 and 12.5 g./10 min., relatively narrow molecular weight distribution, and high bulk density which prevents reactor fouling and facilitates physical handling of the polymer.
DETAILED DESCRIPTION OF THE IN~rENTION
The catalyst of the invention comprises a solid complex component obtained by heating a support of magnesium oxide with methanol, removing all the methanol by drying the support under vacuum, refluxing the treated magnesium oxide with a 1:1 molar mixture of titanium tetrachloride and tetrabutyltitanate, removing any excess titanium compound by washing the support with an inert hydrocarbon solvent, reacting said support containing titanium compound with an organoaluminum compound of formula RnAlX3_n, wherein R is a hydrocarbon radical selected from branched or linear alkyl, alkenyl, cycloalkyl, aryl, alkylaryl or arylalkyl radicals having 1 to 20 carbon atoms, X is hydrogen or halogen, and n is 1, 2 or 3, and aging the resulting supported complex.
rrhe polymerization of ethylene involves subject-ing ethylene in an inert solvent, or in the gas phase, to S Ll ~ ~L
low pressure polymerization conditions in the presence of a catalytic amount of the above-described catalyst and sufficient organoaluminum compound to activate the catalyst and scavenge any undesirable impurities in the system.
The catalyst is prepared by first thoroughly drying the magnesium oxide support by heating under vacuum at temperatures of from 200C. to 6000C. for times up to 24 hours. The dried oxide is then suspended in inert hydrocarbon and stirred for 2 to 4 hours at 600C. with about 20 percent by mole fraction, based on the oxide, of methanol. The support material is then carefully separated from the liquid medium and dried under vacuum. Analysis by infrared shows no alcohol or alcoholate groups remaining on the magnesium oxide at this point. The support is then refluxed with a solution of dibutoxytitanium dichloride in an inert hydrocarbon for 15 to 24 hours. The dibutoxy-titanium dichloride is made by mixing equimolar amounts of titanium tetrachloride and tetrabutyltitanate. me excess titanium compound is removed from the support by repeated washing with the inert hydrocarbon solvent. The resulting magnesium oxide support containing the titanium salt is then dispersed in the inert hydrocarbon, and sufficient organo-aluminum compound added to produce an aluminum to titanium ratio of between 0.05 and 0.5. The organoaluminum compound useful for the catalyst preparation has been described earlier herein and may be, preferably, triethylaluminum, tri-hexylaluminium, triisobutylaluminum, diisobutylaluminum hydride, and the like. The resulting catalyst may be used immediately to polymerize ethylene. It is preferred, however, to age the catalyst for times of 12 S~94 hours to 1 day prior to the polymerization.
The inert hydrocarbon diluent used for preparing the catalyst solutions is that to be used as a reaction medium for the olefin polymerization process. Suitable inert hydrocarbons are the paraffinic and cycloparaffinic hydrocarbons having from 4 to 10 carbon atoms, such as butane, isobutane, pentane, isopentane, hexane, heptane, octane, decane, cyclopenbane, cyclohexane, methylcyclohexane and aromatic hydrocarbons, such as benzene, xylene, toluene and the like. The choice of hydrocarbon may vary with the olefin to be polymerized. The use of hydrocarbons of 6 to 10 carbon atoms will reduce the pressure required for the reaction and may be preferred for safety and equipment cost considerations.
The activator-scavenger used in the polymerization process may be any of the organoaluminum compound known to be useful in Ziegler polymerization systems. The activator may be the same as or different from the organo-aluminum compound used to form the supported catalyst.
The polymerization of ethylene is conveniently carried out in an autoclave or other suitable pressure apparatus. The apparatus is charged with solvent, if used and an activator-scavenger and allowed to equilibrate. The supported catalyst is then added and the reactor pressured with ethylene and a molecular weight regulator such as hydrogen, if used. Polymerization pressures depend mainly on the limitations of the equipment used, but a normal range of pressures would be from 1 to 50 atmospheres with a preferred range of from 6 to 40 atmospheres. Temperatures of polymerization usually are from 400C. to 200C., preferably between 70 and 100C. The catalyst concentration 1~95~94 suitable for the invention are between 0.001 and 10 millimoles of transition metal per liter of solvent, preferably between 0.005 and 0.25 millimoles per liter.
The polyethylenes produced with the catalyst of this invention has melt indices in the injection molding range, i.e. between 3.1 and 12.5 grams per 10 minutes, as measured by ASTM-1238 at 190C. using a 2160 g. applied weight. The molecular weight distirbutions are relatively narrow i.e. 7.6-7.8 as measured by the ratio of melt index at lOK~g weight to the melt index at 2 Kg weight as compared to 8.0-10. for polyethylenes prepared by other supported catalysts. The catalyst of the invention gives a poly-ethylene in the slurry process which has exceptionally high bulk density, i.e. greater than 20 pounds per cubic foot (pcf.), which makes physical handling of the polymer simpler and allows greater amounts of polymer to be produced per unit weight of solvent without the concommitant fouling of the reactor The following examples illustrate, but are not meant to limit the invention.
Example I
a. Catalyst Preparation Anhydrous magnesium oxide was thermally activated by heating under vacuum at 210 to 300C. for 18 hours.
The oxide was then blanketed under purified nitrogen. In a 100 ml Schlenk type flask, 3.8 g. of this activated magnesium oxide was suspended in 60 ml. of n-hexane. To the suspension was added o.76 ml. of methanol and the slurry stirred at 600C. for 2 hours. The solvent was carefully drained off and the solid residue was dried under vacuum. After the solid support was completely dried, purified nitrogen was introduced to blanket the support L~
along with 60 ml. of n-hexane to cover the support.
Infrared analysis showed this support to have no methoxide or free methanol retained at this point.
In a 50 ml. Schlenk type flask, 31.8 millimoles (mm.) of titanium tetrachloride was added to 10 ml. of n-hexane and 29.2 mm. of tetrabutyltitanate was mixed with this solution at room temperature for 5 minutes.
This titanium solution was then added to the support slurry above and refluxed for 21 hours. The liquid was drained out and the solid was washed with 60 ml. portions of hexane five times. A stock solution was made by adding 80 ml. of hexane to the thus formed catalyst slurry.
A preactivated catalyst slurry solution was made by diluting 20 ml. of the stock solution with 20 ml. of hexane and adding 0.73 mm. of triethylaluminum. The pre-activated catalyst slurry solution was then aged for 1 day before use. The catalyst contained 0.34 mm. of titanium per gram of catalyst.
b. Polymerization of Eth~lene Under purified nitrogen atmosphere, 1.5 1. of dry hexane was placed in a 1 gallon autoclave and 6.8 mm.
of triethylaluminum was added as activator-scavenger. The autoclave was heated to 400C. and 1 ml. of the aged, pre-activated catalyst slurry solution was added. The tempera-ture was then raised to 90C. and the reactor pressured to ~5 psig. with hydrogen. The reactor pressure was raised to 150 psig and maintained at that pressure by adding ethylene as needed during the polymerization. The ethylene uptake rate was measured with a stainlesssteelball flowmeter manuf`actured by Matheson. At the end of 2 hours, the 1~5~9~
polymerization was stopped by venting the autoclave, open~
ing the reactor, and filtering the polyethylene from the liquid medium. The ethylene up-take was still 267 units per gram of catalyst at the 2 hour point. The polymer was dried under vacuum at 40O C. overnight. The yield was 207 g. polyethylene, melt index 4.2 g./10 minutes under a load of 2160 g. at 190C., and bulk density of 24.1 pounds per cubic foot (pcf.). The catalyst efficiency was s8,ooo g. PE/g.Ti. The polyethylene had a molecular weight distribution as measured by the ratio of melt index at 10 Kg. weight to the melt index at 2 Kg.weight (MIlo/MI2) of 7.6.
Comparative Example For comparison purposes, the methanol treated magnesium chloride supported catalyst of U.S. 3,642,746 was prepared and utilized as follows:
a. Catalyst Preparation A support of anhydrous magnesium chloride was treated with methanol by the procedure of Example Ia.
Infrared analysis showed the methanol remàined attached to the magnesium chloride after vacuum drying. The support was then refluxed with equimolar amounts of titanium tetra-chloride and tetrabutyltitanate for 21 hours, separated and washed as in Ia. Preactivation with triethylaluminum (aluminum/Titanium = 0.25) gave a catalyst having o.o3 millimoles of titanium per gram of catalyst.
b. Polymerization of Ethylene ~ . .
The procedure of Example Ib. was followed using the above-prepared magnesium chloride supported catalyst and triethylaluminum as activator-scavenger. After two 1~195~94 hours, the ethylene uptake was only 123 units per gram of catalyst (measured by the Matheson flowmeter). The catalyst efficiency was 425,000 g. PE/g. Ti, but the polyethylene formed had a lower melt index of 2.3 g./10 min., a broader distribution of 8.2 (MIlo/MI2), and a low bulk density of 16.9 pcf.
It can thus be seen that the methanol treated magnesium oxide supported catalyst of the present invention, although having lower catalyst efficiency for the first two hours of polymerization than the known methanol-treated magnesium chloride supported catalyst, retains a higher ethylene uptake and hence may have a longer catalyst life.
The polymer prepared by the oxide supported catalyst has better injection molding properties, i.e. higher melt index, higher bulk density, and narrower molecular weight distribution.
3o
. ~
l~SL~]L94 BRIEF SUMMARY OF THE IN~rENTION
It has now been found that a catalyst having high efficiency for polymerizing ethylene is obtained by treating magnesium oxide with methanol, drylng the oxide free of alcohol, impregnating the oxide with a mixture of titanium tetrachloride and tetrabutyltitanate (1:1 mole ratio) and adding an alkylaluminum compound to reduce the titanium mixture. The polyethylene made with this catalyst has melt indices in the injection molding range, i.e. between 3.1 and 12.5 g./10 min., relatively narrow molecular weight distribution, and high bulk density which prevents reactor fouling and facilitates physical handling of the polymer.
DETAILED DESCRIPTION OF THE IN~rENTION
The catalyst of the invention comprises a solid complex component obtained by heating a support of magnesium oxide with methanol, removing all the methanol by drying the support under vacuum, refluxing the treated magnesium oxide with a 1:1 molar mixture of titanium tetrachloride and tetrabutyltitanate, removing any excess titanium compound by washing the support with an inert hydrocarbon solvent, reacting said support containing titanium compound with an organoaluminum compound of formula RnAlX3_n, wherein R is a hydrocarbon radical selected from branched or linear alkyl, alkenyl, cycloalkyl, aryl, alkylaryl or arylalkyl radicals having 1 to 20 carbon atoms, X is hydrogen or halogen, and n is 1, 2 or 3, and aging the resulting supported complex.
rrhe polymerization of ethylene involves subject-ing ethylene in an inert solvent, or in the gas phase, to S Ll ~ ~L
low pressure polymerization conditions in the presence of a catalytic amount of the above-described catalyst and sufficient organoaluminum compound to activate the catalyst and scavenge any undesirable impurities in the system.
The catalyst is prepared by first thoroughly drying the magnesium oxide support by heating under vacuum at temperatures of from 200C. to 6000C. for times up to 24 hours. The dried oxide is then suspended in inert hydrocarbon and stirred for 2 to 4 hours at 600C. with about 20 percent by mole fraction, based on the oxide, of methanol. The support material is then carefully separated from the liquid medium and dried under vacuum. Analysis by infrared shows no alcohol or alcoholate groups remaining on the magnesium oxide at this point. The support is then refluxed with a solution of dibutoxytitanium dichloride in an inert hydrocarbon for 15 to 24 hours. The dibutoxy-titanium dichloride is made by mixing equimolar amounts of titanium tetrachloride and tetrabutyltitanate. me excess titanium compound is removed from the support by repeated washing with the inert hydrocarbon solvent. The resulting magnesium oxide support containing the titanium salt is then dispersed in the inert hydrocarbon, and sufficient organo-aluminum compound added to produce an aluminum to titanium ratio of between 0.05 and 0.5. The organoaluminum compound useful for the catalyst preparation has been described earlier herein and may be, preferably, triethylaluminum, tri-hexylaluminium, triisobutylaluminum, diisobutylaluminum hydride, and the like. The resulting catalyst may be used immediately to polymerize ethylene. It is preferred, however, to age the catalyst for times of 12 S~94 hours to 1 day prior to the polymerization.
The inert hydrocarbon diluent used for preparing the catalyst solutions is that to be used as a reaction medium for the olefin polymerization process. Suitable inert hydrocarbons are the paraffinic and cycloparaffinic hydrocarbons having from 4 to 10 carbon atoms, such as butane, isobutane, pentane, isopentane, hexane, heptane, octane, decane, cyclopenbane, cyclohexane, methylcyclohexane and aromatic hydrocarbons, such as benzene, xylene, toluene and the like. The choice of hydrocarbon may vary with the olefin to be polymerized. The use of hydrocarbons of 6 to 10 carbon atoms will reduce the pressure required for the reaction and may be preferred for safety and equipment cost considerations.
The activator-scavenger used in the polymerization process may be any of the organoaluminum compound known to be useful in Ziegler polymerization systems. The activator may be the same as or different from the organo-aluminum compound used to form the supported catalyst.
The polymerization of ethylene is conveniently carried out in an autoclave or other suitable pressure apparatus. The apparatus is charged with solvent, if used and an activator-scavenger and allowed to equilibrate. The supported catalyst is then added and the reactor pressured with ethylene and a molecular weight regulator such as hydrogen, if used. Polymerization pressures depend mainly on the limitations of the equipment used, but a normal range of pressures would be from 1 to 50 atmospheres with a preferred range of from 6 to 40 atmospheres. Temperatures of polymerization usually are from 400C. to 200C., preferably between 70 and 100C. The catalyst concentration 1~95~94 suitable for the invention are between 0.001 and 10 millimoles of transition metal per liter of solvent, preferably between 0.005 and 0.25 millimoles per liter.
The polyethylenes produced with the catalyst of this invention has melt indices in the injection molding range, i.e. between 3.1 and 12.5 grams per 10 minutes, as measured by ASTM-1238 at 190C. using a 2160 g. applied weight. The molecular weight distirbutions are relatively narrow i.e. 7.6-7.8 as measured by the ratio of melt index at lOK~g weight to the melt index at 2 Kg weight as compared to 8.0-10. for polyethylenes prepared by other supported catalysts. The catalyst of the invention gives a poly-ethylene in the slurry process which has exceptionally high bulk density, i.e. greater than 20 pounds per cubic foot (pcf.), which makes physical handling of the polymer simpler and allows greater amounts of polymer to be produced per unit weight of solvent without the concommitant fouling of the reactor The following examples illustrate, but are not meant to limit the invention.
Example I
a. Catalyst Preparation Anhydrous magnesium oxide was thermally activated by heating under vacuum at 210 to 300C. for 18 hours.
The oxide was then blanketed under purified nitrogen. In a 100 ml Schlenk type flask, 3.8 g. of this activated magnesium oxide was suspended in 60 ml. of n-hexane. To the suspension was added o.76 ml. of methanol and the slurry stirred at 600C. for 2 hours. The solvent was carefully drained off and the solid residue was dried under vacuum. After the solid support was completely dried, purified nitrogen was introduced to blanket the support L~
along with 60 ml. of n-hexane to cover the support.
Infrared analysis showed this support to have no methoxide or free methanol retained at this point.
In a 50 ml. Schlenk type flask, 31.8 millimoles (mm.) of titanium tetrachloride was added to 10 ml. of n-hexane and 29.2 mm. of tetrabutyltitanate was mixed with this solution at room temperature for 5 minutes.
This titanium solution was then added to the support slurry above and refluxed for 21 hours. The liquid was drained out and the solid was washed with 60 ml. portions of hexane five times. A stock solution was made by adding 80 ml. of hexane to the thus formed catalyst slurry.
A preactivated catalyst slurry solution was made by diluting 20 ml. of the stock solution with 20 ml. of hexane and adding 0.73 mm. of triethylaluminum. The pre-activated catalyst slurry solution was then aged for 1 day before use. The catalyst contained 0.34 mm. of titanium per gram of catalyst.
b. Polymerization of Eth~lene Under purified nitrogen atmosphere, 1.5 1. of dry hexane was placed in a 1 gallon autoclave and 6.8 mm.
of triethylaluminum was added as activator-scavenger. The autoclave was heated to 400C. and 1 ml. of the aged, pre-activated catalyst slurry solution was added. The tempera-ture was then raised to 90C. and the reactor pressured to ~5 psig. with hydrogen. The reactor pressure was raised to 150 psig and maintained at that pressure by adding ethylene as needed during the polymerization. The ethylene uptake rate was measured with a stainlesssteelball flowmeter manuf`actured by Matheson. At the end of 2 hours, the 1~5~9~
polymerization was stopped by venting the autoclave, open~
ing the reactor, and filtering the polyethylene from the liquid medium. The ethylene up-take was still 267 units per gram of catalyst at the 2 hour point. The polymer was dried under vacuum at 40O C. overnight. The yield was 207 g. polyethylene, melt index 4.2 g./10 minutes under a load of 2160 g. at 190C., and bulk density of 24.1 pounds per cubic foot (pcf.). The catalyst efficiency was s8,ooo g. PE/g.Ti. The polyethylene had a molecular weight distribution as measured by the ratio of melt index at 10 Kg. weight to the melt index at 2 Kg.weight (MIlo/MI2) of 7.6.
Comparative Example For comparison purposes, the methanol treated magnesium chloride supported catalyst of U.S. 3,642,746 was prepared and utilized as follows:
a. Catalyst Preparation A support of anhydrous magnesium chloride was treated with methanol by the procedure of Example Ia.
Infrared analysis showed the methanol remàined attached to the magnesium chloride after vacuum drying. The support was then refluxed with equimolar amounts of titanium tetra-chloride and tetrabutyltitanate for 21 hours, separated and washed as in Ia. Preactivation with triethylaluminum (aluminum/Titanium = 0.25) gave a catalyst having o.o3 millimoles of titanium per gram of catalyst.
b. Polymerization of Ethylene ~ . .
The procedure of Example Ib. was followed using the above-prepared magnesium chloride supported catalyst and triethylaluminum as activator-scavenger. After two 1~195~94 hours, the ethylene uptake was only 123 units per gram of catalyst (measured by the Matheson flowmeter). The catalyst efficiency was 425,000 g. PE/g. Ti, but the polyethylene formed had a lower melt index of 2.3 g./10 min., a broader distribution of 8.2 (MIlo/MI2), and a low bulk density of 16.9 pcf.
It can thus be seen that the methanol treated magnesium oxide supported catalyst of the present invention, although having lower catalyst efficiency for the first two hours of polymerization than the known methanol-treated magnesium chloride supported catalyst, retains a higher ethylene uptake and hence may have a longer catalyst life.
The polymer prepared by the oxide supported catalyst has better injection molding properties, i.e. higher melt index, higher bulk density, and narrower molecular weight distribution.
3o
Claims (3)
1. A catalyst for the low to intermediate pressure polymerization of ethylene in the presence of an organo-aluminum activator, comprising a solid complex component obtained by heating a support of magnesium oxide with about 20 mole percent of methanol based on oxide, remov-ing all the methanol by drying the support in a vacuum, refluxing the treated magnesium oxide with an excess of an equimolar mixture of titanium tetrachloride and tetra-butyltitanate, removing any excess titanium compound by repeated washing of the support with an inert hydrocarbon solvent, reducing said titanium compound on said support by reacting with a sufficient amount of an organoaluminum compound of formula RnAlX3-n, wherein R is a hydrocarbon radical selected from branched or linear alkyl, alkenyl, cycloalkyl, aryl, alkylaryl or arylalkyl radicals having 1 to 20 carbon atoms, X is hydrogen or halogen, and n is 1, 2 or 3 to form an aluminum to titanium ratio of 0.05 to 0.5, and aging the resulting supported complex.
2. A method for the preparation of a catalyst for the polymerization of olefins which comprises treating an anhydrous magnesium oxide support with about 20 mole percent of methanol based on oxide, removing all the methanol from the magnesium oxide by drying the support under a vacuum, refluxing the treated magnesium oxide with an excess of an equimolar mixture of titanium tetra-chloride and tetrabutyltitanate, removing any excess titanium compound by repeated washing of the support with an inert hydrocarbon solvent, reducing said titanium com-pound on the support by reacting with an organoaluminum compound of formula RnAlX3-n' wherein R is a hydrocarbon radical selected from branched or linear alkyl, alkenyl, cycloalkyl, aryl, alkylaryl or arylalkyl radicals having 1 to 20 carbon atoms, X is hydrogen or halogen, and n is 1, 2 or 3, in an amount such that the aluminum to titanium ratio is between 0.05 and 0.5, and aging the resulting supported complex.
3. A process for the polymerization of ethylene comprising contacting ethylene at a temperature of from 40° to 200°C. at pressures of from 1 to 50 atmospheres in an inert hydrocarbon solvent or in the gas phase with a mixture of an alkylaluminum compound as activator-sca-venger and a supported catalyst made by treating an anhy-drous magnesium oxide support with about 20 mole percent of methanol based on oxide, removing all the methanol from the support by drying the support under a vacuum, refluxing the treated support with an excess of an equi-molar mixture of titanium tetrachloride and tetrabutyl-titanate, removing any excess titanium compound by repeat-ed washing of the support with an inert hydrocarbon sol-vent, reducing said titanium compound on the support by reacting with an organoaluminum compound of formula RnAlX3-n, wherein R is a hydrocarbon radical selected from branched or linear alkyl, alkenyl, cycloalkyl, aryl, alkylaryl or arylalkyl radicals having 1 to 20 carbon atoms, X is hydrogen or halogen, and n is 1, 2 or 3, in an amount such that the aluminum to titanium ratio is be-tween 0.05 and 0.5, and aging the resulting supported complex.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US78013477A | 1977-03-22 | 1977-03-22 | |
| US780,134 | 1985-09-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1095494A true CA1095494A (en) | 1981-02-10 |
Family
ID=25118717
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA287,774A Expired CA1095494A (en) | 1977-03-22 | 1977-09-29 | High efficiency catalyst for high bulk density polyethylene |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS53116293A (en) |
| BE (1) | BE861553A (en) |
| CA (1) | CA1095494A (en) |
| DE (1) | DE2801648A1 (en) |
| FR (1) | FR2384795A1 (en) |
| GB (1) | GB1582110A (en) |
| IT (1) | IT1091773B (en) |
| NL (1) | NL7712002A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4288578A (en) * | 1978-10-12 | 1981-09-08 | Arco Polymers, Inc. | High efficiency catalyst for high bulk density polyethylene |
-
1977
- 1977-09-29 CA CA287,774A patent/CA1095494A/en not_active Expired
- 1977-10-25 JP JP12805977A patent/JPS53116293A/en active Granted
- 1977-11-01 NL NL7712002A patent/NL7712002A/en unknown
- 1977-11-08 IT IT51735/77A patent/IT1091773B/en active
- 1977-12-06 BE BE183210A patent/BE861553A/en not_active IP Right Cessation
- 1977-12-09 FR FR7737162A patent/FR2384795A1/en active Granted
-
1978
- 1978-01-16 DE DE19782801648 patent/DE2801648A1/en not_active Withdrawn
- 1978-03-21 GB GB11179/78A patent/GB1582110A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| NL7712002A (en) | 1978-09-26 |
| BE861553A (en) | 1978-06-06 |
| JPS6123207B2 (en) | 1986-06-04 |
| FR2384795B1 (en) | 1982-03-19 |
| IT1091773B (en) | 1985-07-06 |
| FR2384795A1 (en) | 1978-10-20 |
| GB1582110A (en) | 1980-12-31 |
| JPS53116293A (en) | 1978-10-11 |
| DE2801648A1 (en) | 1978-09-28 |
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