Catalyst for regulating the molecular weight distribution of ethylene polymers.

This invention relates to a vanadium-based catalyst suitable for regulating the molecular weight distribution of ethylene polymers.

U.S. patent 4,508,842 discloses a highly active vanadium-containing catalyst capable of producing ethylene polymers having a broad molecular weight distribution. Said catalyst comprises: <ul id="ul0001" list-style="none"><li>(A) a solid catalyst precursor consisting essentially of <ul id="ul0002" list-style="none"><li>(1) an inorganic carrier, as support for</li><li>(2) the reaction product of (a) a vanadium trihalide and (b) an electron donor, and</li><li>(3) a boron halide or alkyl­aluminum modifier,</li></ul></li><li>(B) an alkylaluminum cocatalyst, and</li><li>(C) a halohydrocarbon polymerization promoter.</li></ul>

The polymers produced in accordance with U.S. patent 4,508,842 have a relatively broad molecular weight distribution, and excellent extrudability. These properties render them extremely useful in a wide variety of applications, such as wire and cable insulation, blow molding, film, and pipe fabrication. However, such polymers cannot be used in other applications, such as injection molding, which require a narrower molecular weight distribution.

U.S. patent 4,514,514, on the other hand, discloses a vanadium-containing catalyst useful in the preparation of ethylene polymers having a narrow molecular weight distribution. Such catalyst comprises: <ul id="ul0003" list-style="none"><li>(A) a solid catalyst component obtained by reacting a tetravalent or pentavalent vanadium halide compound, an organophosphorus compound and an organoaluminum compound.</li><li>(B) an organoaluminum cocatalyst, and</li><li>(C) a halocarbon polymerization activator.</li></ul>

While the catalysts prepared in this manner have been found useful in the preparation of polymers having a narrow molecular weight distribution, such catalysts do not exhibit high polymerization activity unless the vanadium halide compound organophosphorus compound and organoaluminum compound employed to produce catalyst component (A) are reacted together under such conditions that catalyst component (A) is precipitated from solution as a particulate solid. Such procedure, however, results in the formation of irregularly shaped catalyst particles which are undesirable in continuous, commercial polymerization processes, particularly fluid bed polymerizations which require the use of rounded uniform catalyst particles in order to produce rounded polymer particles necessary to sustain polymerization. Rounded catalyst particles of uniform size are usually and conveniently prepared by impregnating the catalyst in a porous inorganic carrier, a procedure precluded by the catalyst preparation process of U.S. patent 4,514,514.

In addition to producing irreqularly shaped catalyst particles, the catalyst preparation procedure of U.S. patent 4,514,514 requires the use of specific ratios of aluminum and phosphorus to effect precipitation of catalyst component (A) from solution. As a result, the relative amounts of aluminum, phosphorus and vanadium in the catalyst cannot be varied as desired. This inflexibility limits the use of the organoaluminum and organophosphorus compounds as catalyst modifiers and the ability to vary polymer properties through the use of these materials.

Japanese Patent Disclosure 61-138605, published June 26, 1986, is similar to U.S. patent 4,514,514 except that an organoaluminum compound is not employed in the preparation of the solid catalyst component. This patent disclosure does not describe the effect of the catalyst produced in accordance therewith on the molecular weight distribution of the polymers produced with it. However, as in U.S. patent 4,514,514, this disclosure requires precipitation of the solid catalyst component from solution and does not permit the use of catalyst supports impregnated with such catalysts.

In accordance with the present invention, it has now been discovered that the molecular weight distribution of ethylene polymers produced employing a vanadium based catalyst system comprising. <ul id="ul0004" list-style="none"><li>(A) a solid catalyst precursor consisting essentially of <ul id="ul0005" list-style="none"><li>(1) a solid, particulate, porous, inorganic carrier, as support for</li><li>(2) the reaction product of (a) a vanadium trihalide and (b) an electron donor, and</li><li>(3) a boron halide or alkyl-­aluminum modifier,</li></ul></li><li>(B) an alkylaluminum cocatalyst, and</li><li>(C) a halohydrocarbon polymerization promoter,</li></ul> can be narrowed and effectively regulated within a wide range by treating catalyst component (A) with varying amounts of a phosphorus-containing compound having the formula: (R)₃P=0 wherein: R is a monovalent hydrocarbon radical free of aliphatic unsaturation containing from 1 to 14 carbon atoms, or -OR¹ wherein R¹ is a monovalent hydrocarbon radical free of aliphatic unsaturation containing from 1 to 14 carbon atoms.

While catalyst component (A) may be treated with the phosphorus-containing compound by simply mixing the two in the polymerization reactor, it is preferred to pre-treat catalyst component (A) with the phosphorus containing compound before it is added to the polymerization reactor.

Thus, the catalyst system of the present invention comprises: <ul id="ul0006" list-style="none"><li>(A) a solid catalyst precursor consisting essentially of <ul id="ul0007" list-style="none"><li>(1) a solid, particulate, porous, inorganic carrier, as support for</li><li>(2) the reaction product of (a) a vanadium trihalide and (b) an electron donor,</li><li>(3) a boron halide or alkyl­aluminum modifier, and</li><li>(4) a phosphorus-containing molecular weight distribution (MWD) requlator having the formula (R)₃P=0, wherein R is as defined above,</li></ul></li><li>(B) an alkylaluminum cocatalyst, and</li><li>(C) a halohydrocarbon polymerization promoter.</li></ul>

As a result of the present invention, it is now possible to effectively regulate the molecular weight distribution (MWD) of ethylene polymers produced by means of a vanadium-containing catalyst system within a wide range by varying the amount of phosphorus-containing compound (R)₃P=0 employed in the preparation of said catalyst system. Surpris­ingly, the catalyst systems containing these phosphorus-containing MWD regulators have been found to be significantly more active than like untreated catalyst systems. As a result, it is possible to produce ethylene polymers by means of these catalyst systems having narrow-to-intermediate molecular weight distributions at enhanced levels of catalyst activity and polymer productivity. By the effective use these phosphorus-containing MWD regulators together with a suitable chain transfer agent, such as hydrogen, to control the molecular weight of the polymers, it is now possible, by means of this system, to tailor polymer properties for use in a wide variety of applications.

The polymers produced with the catalyst system of the present invention have a molecular weight distribution (MWD), defined as the ratio of weight average molecular weight to number average molecular weight (M_w/M_n), of less than 20 to as low as 4. Another means of indicating the molecular weight distribution of a polymer is by the melt flow ratio (MFR) of that polymer. By melt flow ratio is meant the flow index : melt index ratio of the polymer, wherein flow index and melt index are determined in accordance with ASTM-D 1238, Conditions F and E, respectively. The polymers produced with the catalyst system of the present invention have a melt flow ratio of less than 120 to as low as 30. For these polymers, such MFR values correspond to the M_w/M_n values set forth above.

The polymers produced with the catalyst system of the present invention have a melt index of from greater than 0 g/10 minutes to about 500 g/10 minutes, usually of from about 0.1 g/10 minutes to about 100 g/10 minutes. The melt index of a polymer varies inversely with the molecular weight of the polymer, and is a function of the hydrogen/monomer ratio employed during preparation of the polymer.

As indicated above, both the molecular weight and the molecular weight distribution of the polymers can vary widely depending upon the amount of phosphorus-containing MWD regulator present in the catalyst system employed to produce such polymers and the amount of chain transfer agent present during polymerization. As a result, a broad variety of polymers having widely varying properties can be produced.

The polymers produced with the catalyst system of the present invention are also characterized by a density of from about 0.86 g/cm³ to about 0.96 g/cm³. Such polymers generally contain at least 50 mol percent of polymerized ethylene and no more than 50 mol percent of polymerized alpha olefin containing from 3 to 8 carbon atoms and, optionally, polymerized diene. When polymerized diene is present, the polymer ordinarily contains from 0.01 mol percent to 10 mol percent of at least one such diene, from 6 mol percent to 55 mol percent of at least one polymerized alpha olefin containing from 3 to 8 carbon atoms, and from 35 mol percent to 94 mol percent of polymerized ethylene.

Catalyst component (A) consists essentially of: <ul id="ul0008" list-style="none"><li>(1) a solid, particulate, porous, inorganic carrier, as support for</li><li>(2) the reaction product of (a) a vanadium trihalide and (b) an electron donor,</li><li>(3) a boron halide or alkylaluminum modifier, and</li><li>(4) a phosphorus-containing molecular weight distribution (MWD) regulator having the formula (R)₃P=0, wherein R is as defined above.</li></ul>

The vanadium trihalide which is reacted with the electron donor in the preparation of catalyst component (A) is preferable vanadium trichloride, although the halogen present in said vanadium trihalide may be chlorine, bromine or iodine, or any mixture thereof.

The electron donor employed is a liquid, organic Lewis base in which the vanadium trihalide is soluble.

Suitable electron donors include alkyl esters of aliphatic and aromatic carboxylic acids, aliphatic ketones, aliphatic amines, aliphatic alcohols, aliphatic ethers and cycloaliphatic ethers. Particularly useful are alkyl esters of aliphatic carboxylic acids containing from 1 to 4 carbon atoms; alkyl esters of aromatic carboxylic acids containing from 7 to 8 carbon atoms; aliphatic ketones containing from 3 to 6 carbon atoms, preferably from 3 to 4 carbon atoms; aliphatic amines containing from 1 to 14 carbon atoms, preferably from 2 to 8 carbon atoms; aliphatic alcohols containing from 1 to 8 carbon atoms, preferably from 2 to 8 carbon atoms; aliphatic ethers containing from 2 to 8 carbon atoms, preferably from 4 to 5 carbon atoms; and cycloaliphatic ethers containing from 4 to 5 carbon atoms, preferably mono- or di- ethers containing 4 carbon atoms. The aliphatic and cyclo­aliphatic ethers are most preferred, particularly tetrahydrofuran. If desired, these electron donors may be substituted with one or more substituents which are inert under the reaction conditions employed during reaction with the vanadium trihalide, as well as during preparation of and polymerization with catalyst component (A).

The modifier employed in the preparation of catalyst component (A) is a boron halide or alkylaluminum compound having the formula: MX_a wherein: M is boron or AlR²_(3-a) wherein each R² is an alkyl radical containing from 1 to 14 carbon atoms, which radicals may be the same or different, X is selected from the group consisting of fluorine, chlorine, bromine and iodine, and mixtures thereof, and a is an integer having a value of 0, 1 or 2, provided that a is 3 when M is boron.

Preferably any halide present in the modifier is chlorine, and any alkyl radicals present contain from 1 to 6 carbon atoms. Such alkyl radicals may be cyclic, branched or straight chain, and may be substituted with one or more substituents which are inert under the reaction conditions employed during preparation of and polymerization with catalyst component (A). Diethylaluminum chloride is preferred.

The phosphorus-containing compound employed to treat catalyst component (A) so as to regulate the molecular weight distribution (MWD) of the polymers produced with the catalyst of the present invention has the formula: (R)₃P=0 wherein: R is a monovalent hydrocarbon radical free of aliphatic unsaturation containing from 1 to 14 carbon atoms, or -OR¹ wherein R¹ is a monovalent hydrocarbon radical free of aliphatic unsaturation containing from 1 to 14 carbon atoms.

R and R¹ are usually alkyl radicals containing from 1 to 14 carbon atoms, preferably from 1 to 6 carbon atoms, or aryl radicals containirg from 6 to 14 carbon atoms, preferably 6 carbon atoms.

Both R and R¹ may be substituted with one or more substituents which are inert under the reaction conditions employed during treatment of and polymerization with catalyst component (A).

The phosphorus-containing compounds which can be employed to treat catalyst component (A) include both phosphine oxides and phosphates.

Among the phosphine oxides which can be employed are triethylphosphine oxide, tri-<u style="single">n</u> propylphosphine oxide, tributylphosphine oxide, trioctylphosphine oxide, tricyclo­hexylphosphine oxide, triphenylphosphine oxide and tribenzylphosphine oxide.

Illustrative of the phosphates which can be employed are trimethyl phosphate triethyl phosphate, tributyl phosphate, tri-<u style="single">n</u>-amyl phosphate, trihexyl phosphate, triphenyl phosphate and tricresyl phosphate.

A solid, particulate, porous, inorganic material is employed as carrier in the preparation of catalyst component (A). The carrier serves as support for the vanadium trihalide/electron donor reaction product, the boron halide or alkylaluminum modifier, and the phosphorus-containing molecular weight distribution (MWD) regulator. Suitable carriers include inorganic materials, such as oxides of silicon, aluminum and zirconium, as well as phosphates of aluminum. Usually these materials have an average particle size of from about 10 microns to about 250 microns, preferably from about 20 microns to about 150 microns, and a surface area of at least 3 square meters per gram, preferably at least 50 square meters per gram. Polymerization activity of the catalyst i.e., productivity, can be improved by employing a silica support having an average pore size 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.

Catalyst component (A) is prepared by treating a solid, particulate, porous, inorganic carrier with: <ul id="ul0009" list-style="none"><li>(1) the reaction product of (a) a vanadium trihalide and (b) an electron donor,</li><li>(2) a boron halide or alkyl­aluminum modifier, and</li><li>(3) a phosphorus-containing molecular weight distribution (MWD) regulator having the formula (R)₃P=0, wherein R is as defined above.</li></ul>

The vanadium trihalide/electron donor reaction product is prepared by dissolving at least one vanadium trihalide in at least one electron donor at a temperature of from about 20°C up to the boiling point of the electron donor. Dissolution of the vanadium trihalide in the electron donor can be facilitated by stirring, and in some instances by refluxing, the vanadium trihalide in the electron donor. Up to several hours of heating may be required to complete dissolution.

After the vanadium trihalide has been dissolved in the electron donor, the reaction product is impregnated into the carrier. Impreg nation may be effected by adding the carrier to the solution of the vanadium trihalide in the electron donor, and then drying the mixture to remove excess electron donor. The carrier may be added alone as a dry powder or, if desired, as a slurry in additional electron donor. Ordinarily the carrier ard the solution of the vanadium trihalide in the electron donor are mixed together in such amounts that, after drying, the carrier contains from about 0.05 mmoles to about 0.6 mmoles of vanadium per gram, preferably from about 0.3 mmoles to about 0.6 mmoles of vanadium per gram, and most preferably from about 0.3 mmoles to about 0.5 mmoles of vanadium per gram. The impregnated vanadium trihalide/electron donor reaction product prepared in this manner contains from about 1 mole to about 5 moles, preferably from about 2 moles to about 4 moles, and most preferably about 3 moles of electron donor per mole of vanadium trihalide. Excess electron donor not actually complexed with the vanadium trihalide may remain adsorbed on the carrier without ill effects.

The boron halide or alkylaluminum modifier is usually added to the carrier after it has been impregnated with the vanadium trihalide/electron donor reaction product. However, if desired, the boron halide or alkylaluminum modifier may be added to the carrier before it is impregnated with the vanadium trihalide/electron donor reaction product. Addition of the modifier to the carrier may be effected by dissolving one or more modifiers in one or more inert liquid solvents capable of dissolving the modifier, immersing the carrier in the solution, and then drying the mixture to remove the solvent. If the modifier is applied subsequent to the vanadium trihalide/electron donor reaction product, the solvent must be one which does not dissolve the vanadium trihalide/electron donor reaction product. The carrier may be added to the solution of the modifier alone as a dry powder or, if desired, as a slurry in additional inert liquid solvent. Alternatively, the modifier may be added to a slurry of the carrier in the inert liquid solvent. Usually the modifier is added to the slurry dissolved in additional inert liquid solvent, although this is not necessary. Ordinarily the carrier and the solution of the modifier in the inert liquid solvent are mixed together in such amounts that, after drying, the carrier contains from about 0.1 mole to about 10 moles, preferably from about 0.2 mole to about 2.5 moles, of modifier per mole of electron donor in the vanadium trihalide/electron donor reaction product present in the carrier (or to be added to the carrier if it is applied subsequent to the modifier).

Among the solvents which can be employed to dissolve the boron halide or alkylaluminum modifier are hydrocarbon solvents such as isopentane, hexane, heptane, toluene xylene and naphtha.

Addition of the phosphorus-containing compound to the carrier may be effected in the same manner as addition of the modifier, i.e., by dissolving one or more phosphorus-containing compounds in one or more inert liquid solvents capable of dissolving the phosphorus-containing compound, immersing the carrier in the solution, and drying the mixture to remove the solvent. If the phosphorus-containing compound is applied subsequent to the vanadium trihalide/electron donor reaction product, the solvent must be one which does not dissolve the vanadium trihalide/electron donor reaction product. While the phosphorus-containing compound is usually applied separately, for convenience it may be applied together with the modifier in a single solution, provided that the modifier and phosphorus-containing compound employed are not reactive with each other. In any case, the carrier may be added to the solution of the phosphorus-containing compound alone as a dry powder or, if desired, as a slurry in additional inert liquid solvent. Alternatively, the phosphorus-­containing compound may be added to a slurry of the carrier in the inert liquid solvent. Usually the phosphorus-containing compound is added to the slurry dissolved in additional inert liquid solvent, although this is not necessary.

The amount of phosphorus-containing compound employed in the preparation of catalyst component (A) depends upon the particular phosphorus-containing compound employed and the molecular weight distribution desired in the polymers to be produced with the treated catalyst. Catalysts of the type employed herein which have not been treated with a phosphorus-containing compound have been found to produce polymers having a molecular weight distribution (M_w/M_n) in excess of 10 up to about 22 This corresponds to a melt flow ratio (MFR) in excess of 60 up to about 130. By treating such catalysts with the phosphorus-­containing compounds described herein however, it is possible to lower the melt flow ratio (MFR) of the polymers produced up to as much as 50 percent, depending upon the amount of phosphorus-containing compound employed. Reductions of up to 50 percent in melt flow ratio (MFR) usually require a molar ratio of phosphorus-containing compound to vanadium trihalide/electron donor reaction product of from about 1:1 to about 15:1, preferably from about 2:1 to about 10:1. Lesser amounts of phosphorus-containing compound bring about lesser reductions in melt flow ratio (MFR). However, greater amounts of phosphorus-containing compound have not been found to provide any further reduction in melt flow ratio (MFR). Generally, the phosphorus-containing compound is employed in amounts such as to provide a molar ratio of phosphorus-containing compound to vanadium trihalide/electron donor reaction product of from about 0.1:1 to about 30:1, preferably from about 0:2:1 to about 10.1, depending upon the desired result.

As previously disclosed, it is also possible to regulate the molecular weight of the polymers produced by the use of a suitable chain transfer agent, such as hydrogen, during polymerization. Generally, hydrogen is employed and added to the reactor in an amount sufficient to produce a hydrogen:ethylene mol ratio of from about 0.00001:1 to about 0.5:1, depending upon the melt index desired in the polymer product. In addition to hydrogen, other chain transfer agents may be employed to regulate the molecular weight of the polymers.

The ability to regulate the molecular weight distribution of the polymers over a broad molecular weight range allows polymer properties to be tailored for use in multifarious applications and greatly increases the versatility of the catalyst system.

Component (B) of the catalyst system of the present invention is an alkylaluminum cocatalyst having the formula Al(R³)₃ wherein R³ is a saturated hydrocarbon radical containing from 1 to 14 carbon atoms, which radicals may be the same or different. Such radicals may be substituted with one or more substituents which are inert under the reaction conditions employed during polymerization. Preferably R³ is an alkyl radical containing from 2 to 8 carbon atoms.

Component (C) of the catalyst system of the present invention is a halohydrocarbon polymerization promoter having the formula R⁴_bCX′_(4-b) wherein: R⁴ is hydrogen or an unsubstituted or halosubstituted alkyl radical containing from 1 to 6 carbon atoms, which radicals may be the same or different, X′ is halogen, and b is 0, 1 or 2.

Preferred promoters include flouro-, chloro- or bromo- substituted ethane or methane having at least 2 halogens attached to a single carbon atom. Preferred promoters include CCl₄, CHCl₃, CH₂Cl₂, CBr₄, CFCl₃, CH₃CCl₃, and CF₂ClCCl₃. Particularly preferred promoters are CH₃CCl₃, CFCl₃, and CHCl₃.

Polymerization is effected, with the catalyst system of the present invention by contacting ethylene, or a mixture of ethylene and at least one alpha-olefin having 3 to 8 carbon atoms, with the three components of the catalyst system, i.e., the solid catalyst precursor (treated with the phosphorus-containing compound), the alkylaluminum cocatalyst, and the halohydrocarbon polymerization promoter. While polymerization can be effected employing either solution, slurry or gas phase techniques, it is preferably effected in a fluid bed reaction system. Suitable fluid bed reaction systems are described, e.g., in U.S. patent 4,302,565, 4,302,566 and 4,303,771, the disclosures of which are incorporated herein by reference.

The solid catalyst precursor, cocatalyst and polymerization promoter can be introduced into the polymerization reactor through separate feed lines or, if desired two or all of the components may be partially or completely mixed with each other before they are introduced into the reactor. In any event the cocatalyst and polymerization promoter are employed in such amounts as to provide a molar ratio of the promoter to the alkylaluminum cocatalyst of from about 0.1:1 to about 10:1, preferably from about 0.2:1 to about 2:1, and the cocatalyst and the solid catalyst precursor are employed in such amounts as to provide an atomic ratio of aluminum in the cocatalyst to vanadium in the precursor of from about 10:1 to about 400:1, preferably from about 15:1 to about 60:1.

Both the cocatalyst and the polymerization promoter may be introduced into the reactor dissolved in an inert liquid solvent, i.e., a solvent which is nonreactive with all the components of the catalyst system as well as all the components of the reaction system. Hydrocarbons such as isopentane, hexane, heptane, toluene, xylene, naphtha and mineral oil are preferred for this purpose. Generally, such solutions contain from 1 weight percent to 75 weight percent of the cocatalyst and/or the polymerization promoter. If desired, less concentrated or more concentrated solutions can be employed, or, alternatively, the cocatalyst and polymerization promoter can be added in the absence of solvent, or, if desired, suspended in a stream of liquified monomer. When a solvent is employed and polymerization is conducted in a fluid bed, the amount of solvent introduced into the reactor should be carefully controlled so as to avoid the use of excessive quantities of liquid which would interfere with the operation of the fluidized bed.

The solvents employed to dissolve the cocatalyst and the polymerization promoter may also be employed to introduce the solid catalyst precursor into the reactor. Higher boiling solvents, such as mineral oil, are preferred for this purpose. While the solid catalyst precursor may also be introduced into the reactor in the absence of solvent or suspended in liquified monomer, such solvents may be employed to disperse the solid catalyst precursor and facilitate its flow into the reactor. Such dispersions generally contain from 1 weight percent to 75 weight percent of the solid precursor.

The alpha-olefins which may be polymerized with ethylene contain from 3 to 8 carbon atoms per molecule. These alpha olefins should not contain any branching on any of their atoms closer than two carbon atoms removed from the double bond. Suitable alpha-olefins include propylene, butene-1, pentene-1, hexene-1, 4-methyl-pentene-1, heptene-1 and octene-1.

The temperature employed can vary from about 10°C to about 115°C, preferably from about 80°C to about 110°C, when polymerization is effected in gas phase or in a slurry, and from about 150°C to about 250°C when polymerization is effected in a solution. When polymerization is conducted in a fluid bed, the temperature, of course, must be maintained below the sintering temperature of the polymers produced in order to prevent polymer agglomeration.

The pressure employed can vary from subatmosphere to superatmosphere. Pressures of up to about 7000 kPa, preferably of from about 70 kPa to about 3500 kPa, are suitable for gas phase, slurry and solution polymerizations.

If desired, polymerization may be conducted in the presence of an inert gas, i.e., a gas which is nonreactive under the conditions employed during polymerization. The reactor should, however, be maintained substantially free of undesirable catalyst poisons, such as moisture, oxygen, carbon monoxide, carbon dioxide, acetylene, and the like.

When polymerization is conducted in a fluid bed, the superficial gas velocity of the gaseous reaction mixture through the bed must exceed the minimum flow required for fluidization in order to maintain a viable fluidized bed.

The following Examples are designed to illustrate the process of the present invention and are not intended as a limitation upon the scope thereof.

The properties of the polymers produced in the Examples were determined by the following test methods:

Density

A plaque is made and conditioned for one hour at 120°C to approach equilibrium crystallinity and is then quickly cooled to room temperature. Measurement for density is then made in a density gradient column, and density values are reported as grams/cm³.

Melt Index (MI)

ASTM D-1238, Condition E. Measured at 190°C and reported as grams per 10 minutes.

Flow Index (FI)

ASTM D-1238, Condition F. Measured at 10 times the weight used in the melt index text above.

Melt Flow Ratio (MFR)

Ratio of Flow Index : Melt Index.

Activity

Activity values are normalized values based upon grams of polymer produced per mmol of vanadium in the catalyst per hour per 100 psi of ethylene polymerization pressure.

Example 1

Impregnation of Carrier with VCl₃/THF Reaction Product

To a flask equipped with a mechanical stirrer were added 4 liters of anhydrous tetrahydrofuran (THF), followed by 50 grams (0.318 mole) of solid VCl₃. The mixture was heated under nitrogen at a temperature of 65°C for 5 hours with continuous stirring in order to completely dissolve the VCl₃.

Eight hundred grams (800 g) of silica gel were dehydrated by heating under nitrogen at a temperature of 600°C for 20 hours. The dehydrated gel was added to the solution prepared as above, and the mixture was refluxed for one hour under nitrogen. At the end of this time, the mixture was heated at a temperature of 55°C for about 6 hours under a purge of dry nitrogen to produce a dry, free-flowing powder containing about 8 weight percent THF.

Example 2

Treatment of Carrier with Diethylaluminum Chloride

Five hundred grams (500g) of the silica carrier impregnated with VCl₃/THF reaction product in accordance with Example 1 were slurried in 4 liters of anhydrous hexane. The slurry was continuously stirred while a 10 weight percent solution of diethylaluminum chloride in anhydrous hexane was added over a period of 30 minutes. The impregnated carrier and the diethylaluminum chloride solution were employed in amounts that provided a desired atomic ratio of aluminum to vanadium. After addition of the diethylaluminum chloride solution was complete, the mixture was heated at a temperature of 45°C for about 6 hours under a purge of dry nitrogen to produce a dry, free-flowing powder.

Example 3

Treatment of Carrier with MWD Regulator

Five grams (5.0 g) of the silica carrier treated with diethylaluminum chloride in accordance with Example 2 were slurried in 30 ml of anhydrous hexane. The slurry was continuously stirred while a one molar solution of a phosphorus-containing molecular weight distribution (MWD) regulator in anhydrous hexane was added over a period of 5 minutes. After addition of the solution was complete, the mixture was stirred for an additional 30-60 minutes. At the end of this time, the mixture was heated at a temperature of 50°C either under vacuum or under a purge of dry nitrogen to remove the hexane diluent and produce a free-flowing powder.

The procedure was repeated a number of times with various amounts of phosphorus-containing MWD regulators.

Table I below sets forth the particular phosphorus-containing MWD regulators employed in each of these experiments, as well as the molar ratio of MWD regulator to vanadium present in the treated carrier. <tables id="tabl0001" num="0001"><table frame="all"><title>Table I</title><tgroup cols="3" colsep="1" rowsep="0"><colspec colnum="1" colname="col1" colwidth="52.50mm" /><colspec colnum="2" colname="col2" colwidth="52.50mm" /><colspec colnum="3" colname="col3" colwidth="52.50mm" /><thead valign="top"><row><entry namest="col1" nameend="col1" align="left"><u style="single">Example 3</u></entry><entry namest="col2" nameend="col2" align="center"><u style="single">MWD Regulator</u></entry><entry namest="col3" nameend="col3" align="center"><u style="single">Mol. Ratio MWD Regulator to V in Treated Carrier</u></entry></row></thead><tbody valign="top"><row><entry namest="col1" nameend="col1" align="left">(a)</entry><entry namest="col2" nameend="col2" align="left">Tributylphosphine oxide</entry><entry namest="col3" nameend="col3" align="char" char=".">3.7</entry></row><row><entry namest="col1" nameend="col1" align="left">(b)</entry><entry namest="col2" nameend="col2" align="left">Triethyl phosphate</entry><entry namest="col3" nameend="col3" align="char" char=".">4.0</entry></row><row><entry namest="col1" nameend="col1" align="left">(c)</entry><entry namest="col2" nameend="col2" align="left">Tributylphosphine oxide</entry><entry namest="col3" nameend="col3" align="char" char=".">1.6</entry></row><row><entry namest="col1" nameend="col1" align="left">(d)</entry><entry namest="col2" nameend="col2" align="left">Tributylphosphine oxide</entry><entry namest="col3" nameend="col3" align="char" char=".">3.0</entry></row><row><entry namest="col1" nameend="col1" align="left">(e)</entry><entry namest="col2" nameend="col2" align="left">Tributylphosphine oxide</entry><entry namest="col3" nameend="col3" align="char" char=".">3.8</entry></row><row rowsep="1"><entry namest="col1" nameend="col1" align="left">(f)</entry><entry namest="col2" nameend="col2" align="left">Triethyl phosphate</entry><entry namest="col3" nameend="col3" align="char" char=".">3.9</entry></row></tbody></tgroup></table></tables>

Examples 4-15

Slurry Polymerization

The solid catalyst components prepared as described in Example 3 were employed together with an alkylaluminium compound, as cocatalyst, and a halohydrocarbon compound, as polymerization promotor, to co-polymerize ethylene and hexene-1 in a one-liter autoclave reactor.

In each polymerization, the three catalyst components were pre-mixed in a 6 ounce bottle containing 100 ml of hexane before being added to the reactor. Twenty milliliters (20.0 ml) of hexene-1 were added to the pre-mixed catalyst components before the resulting mixture was transferred to the reactor. Anhydrous conditions were maintained at all times.

The polymerization reactor was dried by heating at 96°C under a stream of dry nitrogen for 40 minutes. After cooling the reactor to 50°C, 500 ml of hexane were added to the reactor, and the reactor contents were stirred under a gentle flow of nitrogen. The premixed catalyst components were then transferred to the reactor under a stream of nitrogen and the reactor was sealed. The temperature of the reactor was gradually raised to 60°C and the reactor was pressurized with hydrogen to a pressure of 10 kPa. The temperature was then raised to 75°C and the reactor was pressurized to 1050 kPa with ethylene. Heating was continued until the desired polymerization temperature of 85°C was attained. Polymerization was allowed to continue for 30 minutes, during which time ethylene was continually added to the reactor to maintain the pressure constant. At the end of 30 minutes, the reactor was vented and opened.

Table II below sets forth the details involving the composition of the catalysts employed in these polymerizations, as well as the reaction conditions employed during polymerization, the properties of the polymers produced, and the productivity of each catalyst system.

Shorthand designations employed in Table II are defined as follows: <tables id="tabl0002" num="0002"><table frame="all"><tgroup cols="2" colsep="1" rowsep="0"><colspec colnum="1" colname="col1" colwidth="78.75mm" /><colspec colnum="2" colname="col2" colwidth="78.75mm" /><thead valign="top"><row><entry namest="col1" nameend="col1" align="center"><u style="single">Designation</u></entry><entry namest="col2" nameend="col2" align="center"><u style="single">Definition</u></entry></row></thead><tbody valign="top"><row><entry namest="col1" nameend="col1" align="left">THF</entry><entry namest="col2" nameend="col2" align="left">Tetrahydrofuran</entry></row><row><entry namest="col1" nameend="col1" align="left">DEAC</entry><entry namest="col2" nameend="col2" align="left">Diethylaluminum chloride</entry></row><row><entry namest="col1" nameend="col1" align="left">TBPO</entry><entry namest="col2" nameend="col2" align="left">Tributylphosphine oxide</entry></row><row><entry namest="col1" nameend="col1" align="left">TEOPO</entry><entry namest="col2" nameend="col2" align="left">Triethyl phosphate</entry></row><row><entry namest="col1" nameend="col1" align="left">TEAL</entry><entry namest="col2" nameend="col2" align="left">Triethylaluminum</entry></row><row><entry namest="col1" nameend="col1" align="left">TIBA</entry><entry namest="col2" nameend="col2" align="left">Triisobutylaluminum</entry></row><row rowsep="1"><entry namest="col1" nameend="col1" align="left">TNHAL</entry><entry namest="col2" nameend="col2" align="left">Tri-n-hexylaluminum</entry></row></tbody></tgroup></table></tables>

Comparative Examples A-C

For comparative purposes, ethylene was copolymerized with hexene-1 as in Examples 4-15 employing the solid catalyst component prepared in accordance with Example 2, i.e., the catalyst component employed had not been treated with the MWD regulator as in Example 3. The details of these polymerizations are set forth in Table II below along with the details of Examples 4-15. <tables id="tabl0003" num="0003"><img file="EP0349927A2_D0001.tif" /></tables><tables id="tabl0004" num="0004"><img file="EP0349927A2_D0002.tif" /></tables>