Improved catalyst composition for production of linear low-density ethylene-hexene copolymers and films thereof

Abstract: The invention relates to catalysts composition for polymerizing ethylene alone or in admixture with alpha olefin containing at least three carbon atoms to produce film quality product, wherein the catalyst composition is formed by (i) providing a titanium containing compound which has the empirical formula: MgmTi(OR)nXp(ED)q wherein: R represents a C₁ to C₁₄ aliphatic or C₆ to C₁₄ aromatic hydrocarbon group, or COR′ wherein R′ repesents C₁ to C₁₄ aliphatic or C₆ to C₁₄ aromatic hydrocarbon group; X represents Cl, Br or I, or a mixture thereof; ED represents an electron donor compound; m represents 0.5 to 56, preferably 1.5 to 5; n represents 0, 1 or 2; p represents 2 to 116, preferably 6 to 14, and q represents 2 to 85, preferably 3 to 10. (ii) reacting the titanium containing compound with a reagent system which comprises a methyl aluminum compound comprising dimethyl aluminum chloride or trimethyl aluminum or a mixture thereof and then (iii) combining a product of (ii) with trimethyl aluminum or triethyl aluminum.

Description: The present invention relates to a catalyst for polymerizing olefins, to a method for producing such a catalyst, to a method of polymerizing olefins with such a catalyst, and to films production therewith. A particular aspect of the present invention relates to a catalyst composition which produces linear low density polyethylene (LLDPE) of film production quality, of relatively improved polymer bulk density and narrow molecular weight distribution, and to the polymerization process utilizing such a catalyst composition and to film production therewith whereby the films are characterized by improved dart impact resistance, resin film strength, and reduced FDA extractables. The catalyst comprises a titanium containing compound, treated with a mixture of dimethylaluminum chloride and trimethylaluminum and then combined with triethylaluminum or trimethylaluminum. Polymeric product exhibits excellent bulk density products, comparable to commercial standards, and produces, in film fabrication, films of low FDA extractables, high dart impact resistance and high MD tear strengths. The Catalyst The catalyst compositions employed in the process of the present invention are produced by forming a precursor composition from a magnesium compound, and a titanium compound, preferably in a solvent which may be an electron donor; partially activating the precursor with a mixture of DMAC (dimethylaluminum chloride) and TMA (trimethylaluminum); optionally diluting said precursor composition with an inert carrier; and activating the diluted precursor composition with at least one organoaluminum compound. In accordance with the invention, the organoaluminum compound is provided as triethylaluminum and/or trimethylaluminum. The structure of titanium compound(s) employed in preparing the precursor composition has a formula Ti(OR) a X b wherein R is an aliphatic or aromatic hydrocarbon radical containing from 1 to 14 carbon atoms, or COR' where R' is an aliphatic or aromatic hydrocarbon radical containing from 1 to 14 carbon atoms, X is selected from the group consisting of C1, Br, I, and mixtures thereof, a is 0, 1 or 2, b is 1 to 4 inclusive, and a + b = 3 or 4. Suitable titanium compounds include TiCl 3 , TiCl 4 , Ti(OCH 3 )Cl 3 , Ti(OC 6 H 5 )Cl 3 , Ti(OCOCH 3 )Cl 3 and Ti(OCOC 6 H 5 )Cl 3 . In some instances, TiCl 3 may be preferred because catalysts containing this material show higher activity at the low temperatures and monomer concentrations employed in the process of the present invention. The formula of magnesium compound(s) employed in preparing the precursor composition is MgX 2 wherein X is selected from the group consisting of Cl, Br, I, and mixtures thereof. Suitable magnesium compounds include MgCl 2 , MgBr 2 and MgI 2 . Anhydrous MgCl 2 is particularly preferred. The solvent or electron donor compound(s) employed in preparing the precursor composition is an organic compound which is liquid at 25°C and in which the titanium and magnesium compounds are soluble. The electron donor compounds are known as such, or as Lewis bases. Suitable solvents or electron donor compounds include the alkyl esters of aliphatic and aromatic carboxylic acids, aliphatic ethers, cyclic ethers and aliphatic ketones. Among these electron donor compounds the preferable ones are alkyl esters of saturated aliphatic carboxylic acids containing from 1 to 4 carbon atoms; alkyl esters of aromatic carboxylic acids containing from 7 to 8 carbon atoms; aliphatic ethers containing from 2 to 8 carbons atoms, preferably from 4 to 5 carbon atoms; cyclic ethers containing from 4 to 5 carbon atoms, preferably mono- or di-ethers containing 4 carbon atoms; and aliphatic ketones containing from 3 to 6 carbon atoms, preferably from 3 to 4 carbon atoms. The most preferred of these electron donor compounds include methyl formate, ethyl acetate, butyl acetate, ethyl ether, tetrahydrofuran, dioxane, acetone and methyl ethyl ketone. The precursor composition is formed by dissolving at least one transition metal compound, such as a titanium compound and at least one magnesium compound in at least one electron donor compound at a temperature of from 20°C up to the boiling point of the electron donor compound. Any one or a combination of any of the well known transition metal compounds can be used in preparing the catalyst precursor of this invention. The titanium compound(s) can be added to the electron donor compound(s) before or after the addition of the magnesium compound(s), or concurrent therewith. The dissolution of the titanium compound(s) and the magnesium compound(s) can be facilitated by stirring, and in some instances by refluxing, these two compounds in the electron donor compound(s). After the titanium compound(s) and the magnesium compound(s) are dissolved, the precursor composition may be isolated by crystallization or by precipitation with an aliphatic or aromatic hydrocarbon containing from 5 to 8 carbon atoms, such as hexane, isopentane or benzene. The crystallized or precipitated precursor composition may be isolated in the form of fine, free-flowing particles having an average particle size of from 10 microns to 100 microns after drying at temperatures up to 60°C. 0.5 mol to 56 mols, and preferably 1 mole to about 10 moles, of the magnesium compound(s) are used per mole of the titanium compound(s) in preparing the precursor composition. When thus made as disclosed above the blended or impregnated precursor composition has the formula Mg m Ti(OR) n X p [ED] q wherein R is an aliphatic or aromatic hydrocarbon radical containing from 1 to 14 carbon atoms, or COR' wherein R' is also an aliphatic or aromatic hydrocarbon radical containing from 1 to 14 carbon atoms, X is selected from the group consisting of Cl, Br, I, and mixtures thereof, ED is an electron donor compound, m is 0.5 to 56, preferably 1.5 to 5, n is 0, 1 or 2, p is 2 to 116, preferably 6 to 14, and q is 2 to 85, preferably 3 to 10. After the precursor composition has been prepared it is diluted with an inert carrier material by impregnating such composition into the carrier material. Impregnation of the inert carrier material with the precursor composition may be accomplished by dissolving the precursor composition in the electron donor compound, and then admixing the support with the dissolved precursor composition to impregnate the support. The solvent is then removed by drying at temperatures up to 85°C. The support may also be impregnated with the precursor composition by adding the support to a solution of the chemical raw materials used to form the precursor composition in the electron donor compound, without isolating the precursor composition from said solution. The excess electron donor compound is then removed by drying at temperatures up to about 85°C. Suitably, the impregnated carrier material contains from 3 percent by weight to 50 percent by weight, preferably from 10 percent by weight to 30 percent by weight, of the precursor composition. The carrier materials employed to dilute the precursor composition are solid, particulate, porous materials which are inert to the other components of the catalyst composition, and to the other active components of the reaction system. These carrier materials include inorganic materials such as oxides of silicon and/or aluminum. The carrier materials are used in the form of dry powders having an average particle size of from 10 microns to 250 microns, preferably from 20 microns to 150 microns. These materials are also porous and have a surface area of at least 3 square meters per gram, and preferably at least 50 square meters per gram. Catalyst activity or productivity can apparently be improved by employing a silica support having average pore sizes of at least 80 angstrom units, preferably at least 100 Angstrom units. The carrier material should be dry, that is, free of absorbed water. Drying of the carrier material can be effected by heating, e.g., at a temperature of at least 600°C when silica is employed as the support. Alternatively, when silica is employed, it may be dried at a temperature of at least 200°C and treated with about 1 weight percent to 8 weight percent of one or more of the aluminium activator compounds described below. Modification of the support with an aluminum compound in this manner provides the catalyst composition with increased activity and also improves polymer particle morphology of the resulting ethylene copolymers. In accordance with the invention, the catalyst precursor is partially activated prior to contact with a cocatalyst. That is, the precursor is contacted with a mixture of dimethylaluminum chloride and trimethylaluminum. Preferably, this is undertaken after carrier incorporation into the precursor. This partial activation reaction provides an important control of the early stage of reaction to limit the initial rate of reaction of each catalyst particle so as to control its peak temperature. As is known in the prior art, this has the effect of increasing the bulk density of the resulting polymer. It has been discovered that the partial activation treatment of the invention also has a significant effect on the strength of films produced low density polymerization products. The total amount of prereducing reagent system ranges from 0.1 to 0.8 moles of prereducing agent per mole of THF (tetrahydrofuran) in the un-prereduced precursor. The reagent can be a system including, in addition to those methylaminum compounds described above, triethylaluminum, tri-n-hexylaluminum, and diethylaluminum chloride. The partial activation reaction is preferably carried out in a hydrocarbon solvent slurry followed by drying of the resulting mixture, to remove the solvent, at temperatures of from 20°C to 80°C, preferably from 50°C to 70°C. The resulting product is a free-flowing solid particulate material which can be readily fed to the polymerization reactor where the activation is completed with additional activator compound which can be the same or a different compound as that employed for the partial activation. The partially activated precursor is then reacted with a cocatalyst or activator which is trimethylaluminum (TMA) or triethylaluminum (TEAL) either outside of the reactor vessel or inside the vessel with the catalyst activator. The activator is employed in an amount which is at least effective to promote the polymerization activity of the solid component of the catalyst of this invention. If TMA is employed as the activator, it is preferably used in such amounts that the concentration thereof in the polymer product is 15 to 300 parts per million (ppm), preferably it is 30 to 150 ppm, and most preferably 60 to 100 ppm. If TEAL is employed as the activator, it is preferably used in such amounts that the concentrations thereof in the polymer product is 150 to 500 ppm, and most preferably 250 to 350 ppm. In slurry polymerization processes, a portion of the activator can be employed to pretreat the polymerization medium if desired. The catalyst may be activated in situ by adding the activator and catalyst separately to the polymerization medium. It is also possible to combine the catalyst and activator before the introduction thereof into the polymerization medium, e.g., for up to 2 hours prior to the introduction thereof into the polymerization medium at a temperature of from -40 to 100°C. A suitable activating amount of the activator may be used to promote the polymerization activity of the catalyst. The aforementioned proportions of the activator can also be expressed in terms of the number of moles of activator per gram atom of titanium in the catalyst composition, e.g., from 6 to 80, preferably 8 to 20 moles of TMA activator per gram atom of titanium. The olefin polymerization Higher alpha olefins which can be polymerized with ethylene to produce the low density copolymers of the present invention can contain 3 to 8 carbon atoms. These alpha olefins should not contain any branching on any of their carbon atoms closer than two carbon atoms removed from the double bond. Suitable alpha olefins include propylene, butene-1, pentene-1, hexene-1, 4-methylpentene-1, heptene-1 and octene-1. The preferred alpha olefin is hexene-1. The linear low density polyethylene polymers produced in accordance with the present invention preferably contain at least about 80 percent by weight of ethylene units, preferably at least 88 percent polymerized ethylene. A "diluent" gas is employed with the comonomers. It is nonreactive under the conditions in the polymerization reactor other than to terminate polymer chain growth. In addition, such gas should be insoluble in the polymer product produced so as not to contribute to polymer tackiness. The diluent gas can be hydrogen, nitrogen, argon, helium, methane, ethane, and the like. When hydrogen is employed as a diluent gas, the diluent serves not only to dilute the reaction mixture and prevent polymer agglomeration, but also acts as a chain transfer agent to regulate the melt index of the copolymers produced by the process. Generally, the reaction mixture contains hydrogen in an amount sufficient to produce a hydrogen to ethylene mole ratio of from 0.01:1 to 1.0:1. The molecular weight of the polymer may be controlled in a known manner, e.g., by using hydrogen. With the catalysts produced according to the present invention, molecular weight may be suitably controlled with hydrogen when the polymerization is carried out at relatively low temperatures, e.g., from 70 to 105°C. The molecular weight control is evidenced by a measurable positive change in melt index (I 2 ) of the polymer when the molar ratio of hydrogen to ethylene in the reactor is increased. The average molecular weight of the polymer is also dependent on the amount of the TMA activator employed. Increasing the TMA concentration in the reactor gives small, positive changes in melt index. In addition to hydrogen, other chain transfer agents may be employed to regulate the melt index of the copolymers. Catalyst poisons such as moisture, oxygen, carbon monoxide, carbon dioxide, acetylene and the like should be excluded from the gaseous reaction mixture. Lower concentration of the higher alpha olefin comonomer in the reaction mixture vis-a-vis the ethylene concentration, i.e., the higher the density and modulus of the copolymer being produced, the higher the temperature which can be employed. Exact conditions in the reactor may vary depending depending on the concentration of diluent gas with higher diluent gas concentrations permitting the use of somewhat higher temperature. Temperatures can generally range from 10°C to 80°C. The density of the copolymer is directly related to the temperature. Usually temperatures of 10°C to 60°C are employed to produce copolymers having a density of from 0.86 g/cm 3 to 0.90 g/cm 3 . More elevated temperatures of from 60°C up to 80°C are ordinarily employed in the production of copolymers having a density of from 0.90 g/cm 3 up to 0.91 g/cm 3 . Pressures can range up to 7000 kPa. However, preferably pressures range from 70 kPa to 2500. A particularly desirable method for producing linear low density polyethylene polymers according to the present invention is in a fluid bed reactor. Such a reactor and means for operating the same is described by Levine et al, U.S. Patent No. 4,011,382 and Karol et al, U.S. Patent No. 4,302,566. In fluidized bed reactors, the superficial gas velocity of the gaseous reaction mixture through the bed must exceed the minimum flow required for fluidization, and preferably is at least 0.2 feet per second above the minimum flow. Ordinarily the superficial gas velocity does not exceed 5.0 feet per second, and most usually no more than 2.5 feet per second is sufficient. The copolymer products The copolymer products contain 100 to 1000 ppm, preferably 200 to 800 ppm, residue of the activated catalyst described above. They are low density products characterized by a density ranging from 0.910 to 0.970 g/cm 3 . The polymers prepared in the presence of the catalyst of this invention are linear low density resins. They exhibit relatively low values of melt flow ratio, evidencing a relatively narrow molecular weight distribution, than similar polymers prepared in the presence of previously-known catalyst compositions. Thus, the polymers prepared with the catalysts of this invention are especially suitable for the production of low density, high strength film resins, and low density injection molding resins. The molecular weight distribution of the polymers prepared in the presence of the catalysts of the present invention, as expressed by the melt flow ratio (MFR) values, varies from 24 to 29, preferably from 26 to 27 for LLDPE products having a density of 0.914 to 0.926 gms/cc, and an I 2 melt index of 0.9 to 4.0. As is known to those skilled in the art, such MFR values are indicative of a relatively narrow molecular weight distribution, thereby rendering the polymers especially suitable for low density film applications since the products exhibit less molecular orientation in high-speed film blowing processes, and therefore have greater film strength. They are characterized further by a bulk density of 25 pounds/ft 3 (400 kg/m 3 ). Additionally, the polymer resins produced with the novel catalyst composition of this invention have reduced hexane extractables, and films manufactured from such polymer resins have improved strength properties, as compared to resins and films prepared from resins made with other catalyst compositions. The term "hexane extractables" is used herein to define the amount of a polymer sample extracted by refluxing the sample in hexane in accordance with the FDA-approved procedure. As is known to those skilled in the art, the FDA requires that all polymer products having food contact contain less than 5.5% by weight of such hexane extractables. The polymers produced with the catalyst compositions of the present invention can have 25% lower hexane extractables than the polymers prepared with other catalysts. When fabricated into films, the films exhibit high dart impact resistance. Dart impact resistance or dart drop is defined herein by A.S.T.M. D-1709, Method A; with a 38.1 mm dart, and a drop height of 0.66 meters. For example, the films of the present invention exhibit significant improvement in dart drop and machine dimension (MD) tear properties than the films prepared with previously-known catalysts. The resins prepared with the catalyst of the invention may have higher settled bulk densities than the resins prepared with similar catalysts synthesized with TEAL or other prior art activators, and may have substantially improved higher alpha-olefins, e.g., 1-hexene, incorporation properties, as compared to different catalyst compositions. The properties of the polymers produced in the Examples were determined by the following test methods: Density ASTM D-1505 - A plaque is made and conditioned for one hour at 100°C to approach equilibrium crystallinity. Measurement for density is then made in a density gradient column; reported as gms/cc Melt Index (MI), I 2 ASTM D-1238- Condition E - Measured at 190°C - reported as grams per 10 minutes. High Load Melt ASTM D-1238 - Condition F - Measured at Index, I 21 10.5 (HLMI), I 21 times the weight used in the melt index test above. Melt Flow Ratio = (MFR) I 21 I 2 Productivity A sample of the resin product is ashed, and the weight % of ash is determined; since the ash is essentially composed of the catalyst, the productivity is thus the pounds of polymer produced per pound of total catalyst consumed. The amount of Ti, Mg and Cl in the ash are determined by elemental analysis. Settled Bulk Density The resin is poured via 1" diameter funnel into a 100 mil graduated cylinder to 100 mil line without shaking the cylinder, and weighed by difference. The cylinder is then vibrated for 5-10 minutes until the resin level drops to a final, steady-state level. The settled bulk density is taken as the indicated cylinder volume at the settled level, divided by the measured resin weight. n-hexane extractables (FDA test used for polyethylene film intended for food contact applications). A 200 square inch (0.13 m 2 ) sample of 1.5 mil (0.038 mm) gauge film is cut into strips measuring 1" x 6" (2.5 x 15cm) and weighed to the nearest 0.1 mg. The strips are placed in a vessel and extracted with 300 ml of n-hexane at 50 ± 1°C for 2 hours. The extact is then decanted into tared culture dishes. After drying the extract in a vacuum dessicator the culture dish is weighed to the nearest 0.1 mg. The extractables, normalized with respect to the original sample weight, is then reported as the weight fraction of n-hexane extractables. Machine Direction Tear, MD TEAR (gm/mil) ASTM D-1922 EXAMPLES Precursors loaded with Magnesium (MgCl 2 ) and Titanium (TiCl 3 ) were tested. The Mg/Ti ratio ranged from about 3.2 to about 5. These were formed in accordance with the description of Levine et al, U.S. Patent No. 4,719,193. Table I lists the catalyst compositions and the pilot plant fluid bed results. Catalysts 1 through 5 were prepared from the same batch of precursor, and partially activated with different combinations of aluminum alkyls and alkylaluminum chlorides. The combinations were 1) diethylaluminum chloride (DEAC) and tri-n-hexylaluminum (TnHAL), which is the commercial standard, 2) DEAC and triethylaluminum (TEAL), 5) DEAC and trimethylaluminum (TMA), 3) dimethylaluminum chloride (DMAC) and TnHAL, and 4) DMAC and TMA. These five catalysts each contained approximately the same molar amounts of the two activating alkyls. Table I identifies the reagent loadings expressed as a molar ratio of added alkyl to the THF (tetrahydrofuran) in the un-prereduced precursor. Catalyst Number 1, the commercial standard, had a somewhat lower loading of DEAC than planned, 0.33 moles/mole compared with the average 0.45. In table I, catalyst nos. 1,2,3 and 5 represent comparative examples. EXPERIMENTAL CONDITIONS AND RESULTS Catalyst 1 2 3 4 5 Reducing Agents Alkyl #1 DEAC DEAC DMAC DMAC DEAC Alkyl #2 TnHAC TEAL TnHAL TMA TMA Catalyst Compositions Mg (wt%) 2.10 2.39 2.04 2.46 2.46 Ti (wt%) 1.27 1.47 1.30 1.50 1.50 Al (wt%) 4.78 5.49 4.82 5.77 6.32 Cl (wt%) 9.56 10.1 10.0 10.3 9.57 THA (wt%) 10 11 12 12 11 Alkyl #1 (mol/mol THF) 0.33 0.48 0.44 0.46 0.46 Alkyl #2 (mol/mol THF) 0.24 0.24 0.22 0.23 0.22 Operating Conditions C 2 PSI 93 91 96 103 100 C 6 /C 2 mol ratio 0.151 0.153 0.149 0.151 0.150 H 2 /C 2 mol ratio 0.164 0.149 0.145 0.152 0.165 Residence Time (h) 3.7 3.6 3.6 3.8 3.6 Cocatalyst (TMA) feed (gms/10 6 gm. product) 91 96 88 87 83 Properties Melt Index (dg/min) 0.96 1.17 1.0 1.0 0.94 Melt Flow Ratio 27.2 27.4 27.6 26.2 26.6 Density (g/cc) 0.9170 0.9173 0.9168 0.9180 0.9190 Settled Bulk Den (lb/ft 3 ) (Den (kg/m 3 ) 24.9 399 25.2 404 25.5 409 25.0 400 25.2 404 Ti (ggm) 3.4 2.4 2.4 3.3 2.2 Film Properties FDA Extractables (wt%) 3.8 4.3 4.0 3.0 3.0 Dart Impact (g) 340 310 340 330 350 MD Tear (gm/mil) 420 460 450 480 460 The catalysts were tested in the pilot plant fluid bed reactor under substantially equivalent conditions (Table I). The catalyst activator used in all experiments was TMA. The feed rate of TMA was 80 to 100 (83-96) ppm based on the resin production rate. Other reaction conditions were: 88°C reaction temperature, 111 pound (50 kg) bed weight, 31 lb/hour (14 kg/hr) ethylene feed. The H 2 /C 2 molar ratio was adjusted to between 0.14 and 0.17, and hexene feed between 5.6 and 5.9 lb/hour (2.5 to 2.6 kg/hr) to maintain product specifications. The target was a .9170 to .9190 ASTM density, 0.9 to 1.1 melt index resin. Consequently, pilot plant QC densities ranged between 0.915 and 0.917, and flow indices between 22 and 29. Resin samples from the pilot plant were fabricated into film, and the physical properties were measured by standard ASTM methods. Results are shown at the bottom of Table I. These data were then corrected to account for small experimental differences in resin density and melt index and presented in Table II. As is known to persons skilled in the art, the properties of polyethylene film are sensitive to variations in resin density and melt index. The corrections were done to remove these effects from the data of Examples 1 through 5, so as to isolate the effects of the catalyst changes. The corrections were carried by the generally recognized methods described by Schurzky, Journal of Plastic Film & Sheeting, Vol. 1, pp 142-151, April 1985, the entire contents of which are incorporated herein by reference. In Table II, examples 1,2,4 and 5 are comparative examples. Results indicate that if the reactor products had exactly the same density and melt index then: 1. Replacing DEAC with DMAC lowers extractables 7% and raises dart impact resistance and MD tear strength 10% (catalysts 1 vs 2). 2. Replacing TnHAL with TMA raises dart impact 5% and MD tear 8% (catalysts 1 vs 4). 3. Replacing both DEAC and TnHAL with DMAC and TMA lowers FDA extractables 13% and raises dart impact and MD tear 15% (catalysts 1 vs 3). 4. Polymer bulk density was not affected by the change in alkyls (Table I). For film evaluation, each sample was compounded on a 25 pound Banbury, at mild conditions, with 600 ppm Irganox 1076, 1000 ppm PEPQ, and 500 ppm, each, zinc stearate and AS990. Film was then fabricated on the 2-1/2 inch Sterling extruder at 1.5 mil film gauge, 430°F (221°C) melt temperature, 100 mil (2.5 mm) die gap, 2:1 BUR, and 6 pounds/hour inch (1 kg/hr.cm) of die. COMPARATIVE PRODUCT PROPERTIES (Corrected for Density and MI Variations) (c) Activating Agent FDA Relative Relative Alkyl Groups Extractables Dart Impact MD Tear Alkyl #1 Alkyl #2 (wt%) 1 DEAC TnHAL 3.0 1.00 1.00 2 DMAC TnHAL 2.8 1.10 1.11 3 DMAC TMA 2.6 1.15 1.15 4 DEAC TMA 3.0 1.05 1.08 5 DEAC TEAL 3.2 1.04 1.10

Claims: A catalyst composition for polymerizing ethylene alone or in admixture with alpha olefin containing at least three carbon atoms to produce film quality product, wherein the catalyst composition is formed by (i) providing a titanium containing compound which has the empirical formula: Mg m Ti(OR) n X p [ED] q wherein: R represents a C 1 to C 14 aliphatic or C 6 to C 14 aromatic hydrocarbon group, or COR' wherein R' represents a C 1 to C 14 aliphatic or C 6 to C 14 aromatic hydrocarbon group; X represents Cl, Br or I, or a mixture thereof; ED represents an electron donor compound; m represents 0.5 to 56, preferably 1.5 to 5; n represents 0, 1 or 2; p represents 2 to 116, preferably 6 to 14, and q represents 2 to 85, preferably 3 to 10. (ii) reacting the titanium containing compound with a reagent system which comprises a mixture of dimethyl aluminum chloride and trimethyl aluminum and then (iii) combining a product of (ii) with trimethyl aluminum or triethyl aluminum. A catalyst composition according to Claim 1, wherein said reagent system further includes tri-n-hexylaluminum. A catalyst composition according to Claim 1 or 2, wherein the titanium-containing compound is produced by reacting Ti(OR) a X b with MgX 2 wherein: R and X are defined in claim 1; a represents 0, 1 or 2; b represents a number from 1 to 4; and a + b = 3 or 4.

Inventors: COOK PAMELA JEAN, HAGERTY ROBERT OLDS, HUSBY PER KRISTIAN, NOWLIN THOMAS EDWARD, COOK, PAMELA JEAN, HAGERTY, ROBERT OLDS, HUSBY, PER KRISTIAN, NOWLIN, THOMAS EDWARD
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1992
Main classification: C08F210
IPC codes: C08F4, C08F10, C08F210, C08J5