Process for olefin polymerization

Abstract: Novel chromium-containing compounds are prepared by forming a mixture of a chromium salt, a metal amide, and an ether. These novel chromium-containing, or chromium pyrrolide, compounds can be used as a cocatalyst in the presence of an olefin polymerization catalyst to produce a comonomer in-situ. The resultant polymer, although produced from predominately one monomer, has characteristics of a copolymer.

Description: BACKGROUND OF THE INVENTION This invention relates to the polymerization of olefins, such as ethylene, in the presence of any polymerization catalyst and one or more novel chromium cocatalysts. It is well known that olefins, such as ethylene, can be polymerized with catalyst systems employing supported, chromium catalysts or magnesium/titanium catalysts. Initially such catalysts were used primarily to form olefin homopolymers. It soon developed, however, that many applications required polymers which were more impact resistant than olefin homopolymers. Consequently, in order to produce polymer having short chain branching like the more flexible free radical polymerised olefin polymers, comonomers such as propylene, butene, hexene or the higher olefins were copolymerized with the olefin monomer to provide resins tailored to specific end uses. The copolymers, however, are more expensive to produce since inventories of different monomers must be kept and also the comonomers are generally more expensive than the usual short-chain monomers, such as ethylene or propylene. Linear olefin polymers, such as ethylene, with short chain branching can be formed from a pure ethylene feed using the old free radical high pressure process, but the conditions necessary to do this make the product too expensive to he commercially competitive. Additional control over the polymerization process and the resultant polymer is also desired. A process to consistently reduce the density of linear olefin polymers and to more efficiently produce and incorporate comonomers into the linear olefin polymer is economically advantageous. A shift in the polymer branch distribution, wherein the branch length is decreased and the amount of branching is increased, is also economically desirable. SUMMARY OF THE INVENTION Accordingly it is an object of this invention to provide a low cost route to linear olefin polymers having toughness imparted by short chain branching. It is a further object of this invention to provide a process by which olefin polymers having the properties associated with copolymers can be obtained from a pure, single olefin feed. It is yet a further object of this invention to provide an improved polymerization process. It is a further object of this invention to provide a novel polymerization process to control polymer density. It is yet a further object of this invention to provide a novel polymerization process to improve comonomer production and incorporation into olefin polymers. It is a further object of this invention to provide a novel polymerization process to shift olefin distribution. It is a further object of this invention to provide a novel polymerization process to control polymer short chain branching. In accordance with this invention, an essentially pure, single olefin feed is contacted under polymerization conditions with a polymerization catalyst and an olefin trimerization cocatalyst comprising the reaction product of a chromium salt, A metal amide, and an ether. Additionally, hydrogen car be introduced into the polymerization reactor in an amount sufficient to accelerate the trimerization and/or polymerization processes. BRIEF DESCRIPTION OF THE DRAWINGS FIGURE I is a computer generated, simplified structural formula of a molecule of Product I, Cr₅(NC₄H₄)₁₀(OC₄H₈)₄, as determined by single crystal x-ray crystallography, and FIGURE II is a further simplified structural representation of the same molecule shown in FIGURE I. FIGURE III is a computer generated simplified structural formula of a molecule of Product III, Cr(NC₄H₄)₄, as determined by single crystal x-ray crystallography. FIGURE IV is a further simplified structural representation of the same molecule shown in Figure III, however, the entire crystal lattice, with the formula [Cr(NC₄H₄)₄][Na]₂·2(OC₄H₈) is shown. FIGURE V is a computer generated, simplified structural formula of a molecule of Product IV, Cr(NC₄H₄)₅(OC₄H₈) as determined by single crystal x-ray crystallography, and FIGURE VI is a further simplified structural representation of the same molecule shown in FIGURE V, however the entire crystal lattice, with the formula [Cr(NC₄H₄)₅(OC₄H₈)][Na]₂·4(OC₄H₈), is shown. DETAILED DESCRIPTION OF THE INVENTION Polymerization Catalyst The inventive chromium compounds can be used either supported or unsupported as a cocatalyst with any other olefin polymerization catalyst. Generally, polymerization catalysts are considered either chromium catalysts (also known as "Phillips Catalysts") or titanium and/or vanadium-containing catalysts. Any chromium catalyst known in the art can be used. Exemplary chromium catalysts are disclosed in U.S. Patents 3,887,494; 3,900,457; 4,053,436; 4,151,122; 4,294,724; 4,392,990; and 4,405,501. Any titanium and/or vanadium-containing catalyst known in the art can also be used. Exemplary magnesium/titanium catalysts are disclosed in U.S. Patents 4,394,291; 4,326,988; and 4,347,158. A preferred polymerization catalyst is a supported chromium catalyst. The amount of inventive chromium compound used as a cocatalyst can be any amount sufficient to generate a comonomer that can be incorporated into the polymer product. The Chromium Compounds The inventive chromium compounds, which can be used preferably for olefin trimerization and, optionally, olefin polymerization, can be produced by forming a reaction mixture comprising a chromium salt, a metal amide, and an ether. As used in this disclosure, the inventive chromium compounds are referred to by a variety of names, such as inventive or novel chromium compound(s), chromium complex(es), chromium pyrrole complex(es) and/or chromium pyrrolide. The chromium salt can be one or more organic or inorganic chromium salts, wherein the chromium oxidation state is from 0 to 6. As used in this disclosure, chromium metal is included in this definition of a chromium salt. Generally, the chromium salt will have a formula of CrX n . wherein X can be the same or different and can be any organic or inorganic radical, and n is an integer from 1 to 6. Exemplary organic radicals can have from 1 to 20 carbon atoms, and are selected from the group consisting of alkoxy, ester, ketone, and/or amido radicals. The organic radicals can be straight-chained or branched, cyclic or acyclic, aromatic or aliphatic, and can be made of mixed aliphatic, aromatic, and/or cycloaliphatic groups. Exemplary inorganic radicals include, but are not limited to halides, sulfates, and/or oxides. Preferably, the chromium salt is a halide, such as, for example chromous bromide, chromic bromide, chromous iodide, chromic iodide, chromous flouride, chromic flouride, chromous chloride, chromic chloride, and mixtures thereof. Most preferably, the chromium salt is a chloride, such as, for example chromous chloride and/or chromic chloride, due to simple separation of the reaction by-products such as, for example, sodium chloride, as well as relatively low cost. The metal amide can be any metal amide that will react a chromium salt to form a chromium-amido complex. Broadly, the metal amide can be any heteroleptic or homoleptic metal complex or salt, wherein the amide radical can be any nitrogen-containing organic radical. Generally, the metal amide will have from 1 to 20 carbon atoms. Exemplary metal amides include, but are not limited to, primary and/or secondary amines, any alkali metal (Group IA of the Periodic Table) amide and/or any alkaline earth metal (Group IIA of the Periodic Table) amide. The hydrocarbyl portion of the salt of the metal amide is selected from the group consisting of straight chain or branched, cyclic or acyclic, aromatic or aliphatic, and mixtures of two or more thereof. Preferably, the metal amid is selected from a Group IA or Group IIA metal amide, due to ease of reaction with chromium halides. Exemplary preferred metal amides include, but are not limited to, lithium dimethylamide, lithium diethylamide, lithium diisopropylamide, lithium dicyclohexylamide, sodium bis(trimethylsilyl)amide, sodium indolide, sodium pyrrolide, and mixtures of two or more thereof. Most preferably, the metal amide is selected from the group consisting of sodium pyrrolide, lithium pyrrolide, and/or the salts of substituted pyrrolides, because of high reactivity and activity with the other reactants. Examples of salts of substituted pyrrolides include, but are not limited to sodium 2,5-dimethyl pyrrolide and/or 3,4-dimethyl pyrrolide. The ether in the reaction mixture can be one or more ether compounds to affect a reaction between the chromium salt and the metal amide. While not wishing to he bound by theory, it is believed that the ether can be a reaction solvent, as well as a possible reactant. The ether can be any aliphatic and/or aromatic compound containing an R-O-R functionality, wherein the R groups can be the same or different, but is not hydrogen. Preferred ethers are aliphatic ethers, for safety reasons in that aromatic ethers are human toxins. Furthermore, the preferred ethers are those which facilitate a reaction between a chromium halide and a Group IA or Group IIA metal pyrrolide, and also can be easily removed from the reaction mixture. Exemplary compounds include, but are not limited to, tetrahydrofuran, dioxane, diethylether, dimethoxyethane, diglyme, triglyme, and mixtures of two or more thereof. Most preferably, the ether is selected from the group consisting of tetrahydrofuran, derivatives of tetrahydrofuran, dimethoxyethane, derivatives of dimethoxyethane, and mixtures thereof, for the reasons given above, as well as that the preferred salt of an amino is soluble in these ethers. The amount of each reactant used to prepare one or more of the novel chromium compounds can vary, based on the desired chromium compound product. Any amount of each reactant can be used to produce the novel chromium compounds, depending on the desired product. Different reaction stoichiometrics can produce different chromium compounds. For example, the reaction of one mole of chromium (II) with two moles of sodium pyrrollide can produce different products than reacting one mole of chromium (II) with an excess of sodium pyrollide. Furthermore, as stated earlier, selection of different, although similar reactants, can produce different products. For example, using either tetrahydrofuran or dimethoxyethane can result in a different reaction product. The three reactants can be combined in any manner under conditions suitable to form a solution comprising one or more of the inventive chromium compounds. The reaction preferably occurs in the absence of oxygen and therefore under an inert gas, such as, for example, nitrogen and/or argon. The reaction pressure can be any pressure sufficient to maintain the reactants in a liquid state. Generally, pressures within the range of from atmospheric pressure to three atmospheres are acceptable. For ease of operation atmospheric pressure is generally employed. The reaction temperature can be any temperature which maintains the ether in a liquid form. In order to effectuate a more efficient reaction, temperatures near the boiling point of the ether are preferred. Most preferably, the reaction temperature is at the boiling point of the ether and the reaction mixture is refluxed for a period of time. The reaction time can be any amount of time necessary for the reaction to occur. Depending on the reactants, as well as the reaction temperature and pressure, reaction time can vary from 1 minute to 1 week. Usually, reaction time ranges from 3 hours to 5 days. Under optimum conditions, the reaction time can be within the range of from 3 to 48 hours. After the reaction is complete, a solid reaction product can be recovered by any method known in the art. Preferably, though not required, upon completion of the reaction, the reaction mixture first is filtered to remove any reaction by-products such as, for example, salts, like sodium chloride, prior to any other treatment. Although removal of any reaction by-products is not necessary, such removal preferably is done in order to expedite later purification of the chromium product. After filtering, one exemplary method to recover a solid reaction product is to remove the excess ether from the reaction mixture. The excess ether can be removed according to any method known in the art. Exemplary ether removal methods include, but are not limited to, slow evaporation, under vacuum and/or a nitrogen purge. Other ether removal procedures can he used either alone or in combination. For example, the reaction mixture can be filtered and then vacuum dried. Preferably, the reaction mixture is heated slowly and maintained at temperature within the range of 10° to 300°C, preferably 25° to 200°C, under a vacuum, for safety, to remove the excess ether. The resultant solid reaction product is one or more of the inventive chromium compounds. Alternatively, the reaction mixture can be filtered to remove any solid reaction by-product and the filtered reaction mixture can be contacted with a non-polar organic solvent. Addition of a non-polar organic solvent causes one or more of the inventive chromium compounds to form a solid precipitate. Exemplary non-polar organic solvents include, hut are not limited to, pentane, hexane, cyclohexane, heptane, and mixtures thereof. Most preferably pentane is added to the filtered reaction mixture because of the availability and ease of use. The precipitated inventive chromium compounds can be recovered by any method known in the art. The simplest procedure to recover the inventive precipitated chromium compounds is by filtration. The reaction mixture and the resultant solid reaction products, as stated earlier, are kept in an oxygen-free atmosphere at all times. Preferably, due to availability and ease of use, an inert atmosphere such as, for example, nitrogen, is the ambient. Numerous chromium compounds can be prepared in accordance to the invention, by varying the reactants and/or the quantity of each reactant employed. The recovered, novel chromium compound or compounds can be used for olefin trimerization and/or polymerization without further purification. Optionally, the chromium compound can be purified in accordance with any method known in the art. For example, one of the simplest purification procedures is to wash the recovered solid with a non-polar organic solvent such as, for example, toluene. Preferably, a non-polar aliphatic organic solvent is used for best results. Exemplary wash solvents include, but are not limited to, pentane, hexane, cyclohexane, heptane, and mixtures thereof. Most preferably, pentane is the wash solvent. The inventive chromium compounds can be used as supported and/or unsupported catalyst for olefin trimerization and/or polymerization. A supported chromium catalyst can be prepared according to any method known in the art. Any support useful to support chromium catalyst can be used. Exemplary catalyst supports include, but are not limited to, inorganic oxides, either alone or in combination, phosphated inorganic oxides, and mixtures thereof. Particularly preferred are supports selected from the group consisting of silica, silica-alumina, alumina, fluorided alumina, silated alumina, thoria, aluminophosphate, aluminum phosphate, phosphated silica, phosphated alumina, silica-titania, coprecipitated silica/titania, and mixtures, thereof, fluorided/silated alumina, being presently preferred, as well as any one or more of these supports which can contain chromium. The presently most preferred catalyst support is because of the greatest trimerization activity, is aluminophosphate, as disclosed in U.S. Patent 4,364,855 (1982). The supported chromium catalyst system can be prepared according to any method known in the art. For example, the reaction mixture, which preferably has been filtered to remove any particulate reaction by-products and contains one or more of the novel chromium pyrrolide compounds, is combined and thoroughly contacted with a catalyst support. Excess ether does not have to be removed prior to contacting the catalyst support. However, a solid chromium pyrrolide compound can be re-dissolved in an ether, if desired. The chromium pyrrolide/ether solution is usually a blue or blue/green color. The catalyst support usually is insoluble in the ether/chromium pyrrolide complex solution. Any excess of the chromium pyrrolide in relation to the catalyst support is sufficient. However, usually, at least 5 grams of chromium pyrrolide compound per gram of catalyst support is sufficient. Preferably 0.001 to 1 grams of chromium pyrrolide compound per gram of support, and most preferably 0.01 to 0.5 grams of chromium pyrrolide compound per gram of support is used for best support loading and most efficient use of the reagents. This mixture can be contacted and mixed at any time, temperature, and pressure to thoroughly contact the chromium pyrrolide compound and support. For ease of use, ambient temperatures and pressures are preferred. Mixing times can be up to 24 hours, preferably 5 seconds to 10 hours, and most preferably 5 seconds to 8 hours. Longer times usually provide no additional benefit and shorter times can be insufficient for thorough contacting. After the support is added and thoroughly combined with the chromium pyrrolide it is collected by filtration, vacuum dried, then a solution of one or more Lewis acids, preferably in a hydrocarbon solvent, is added to the support/chromium pyrrolide mixture. As used in this disclosure, a Lewis acid is defined as any compound that is an electron acceptor. Preferred Lewis acids include, but are not limited to, alkylaluminum compounds, derivatives of alkylaluminum compounds, halogenated alkylaluminum compounds, and mixtures thereof. Exemplary compounds include, but are not limited to, triethylaluminum, diethylaluminum, ethylaluminum sesquichloride, and mixtures thereof. The most preferred alkylaluminum compound is triethylaluminum, for best results in catalyst activity. The hydrocarbon solvent can be any hydrocarbon that will dissolve the Lewis acid. Preferred hydrocarbons include, but are not limited to, aromatic compounds having about 6 to 50 carbon atoms per molecule. Most preferably, the hydrocarbon solvent is toluene, for ease of removal and minimal interference with the resultant catalyst. Any amount of Lewis acid is sufficient to activate and/or react with the chromium pyrrolide catalyst. Usually 200 moles of Lewis acid per gram of chromium can be used. Preferably, 1 to 100 grams of Lewis acid per gram of chromium pyrrolide, and most preferably 5 to 30 grams of Lewis acid per gram of chromium pyrrolide are used, for best catalyst activity. However, the amount of Lewis acid employed can vary with the catalyst support used. For example, if the support is silica and/or alumina, too much Lewis acid can decrease catalyst activity. However, a similar amount of Lewis acid used with an aluminophosphate support does not always significantly decrease catalyst activity. As disclosed earlier, the mixture of chromium pyrrolide, catalyst support, and Lewis acid are mixed and/or contacted under a dry, inert atmosphere at all times. Any pressure can be used during the contacting; for ease of use, atmospheric pressure is preferred. Any temperature can be used during the contacting; for ease of use, room temperature, or ambient temperature, is preferred. Some care should be taken during the mixing, so as not to destroy the physical integrity of the chromium pyrrolide, catalyst support, and resultant supported catalyst. The three-component mixture can he contacted for any amount of time sufficient to prepare and activate a chromium catalyst. Usually times in the range of about one minute to about one week are sufficient. Preferably, times in the range of 30 minutes to 24 hours are used, and most preferably times in the range of one hour to 12 hours are used. Too short of mixing times can result in incomplete contacting and too long of mixing times will not provide any additional catalytic benefit. An alternative, and presently preferred, method to produce a supported catalyst is to combine one or more solid, inventive chromium pyrrolide compounds with a hydrocarbon solvent, as disclosed earlier, such as, for example, toluene, and a Lewis acid, as disclosed earlier, such as, for example, triethylaluminum. This mixture can be stirred for any time sufficient to dissolve the chromium pyrrolide compound, at any pressure or temperature. Usually, times of one minute to one week, preferably one hour to 24 hours, and most preferably within the range of three hours to 12 hours are used. For ease of operation, ambient temperatures and pressures are used. Usually, a brown solution will result. After the solution is sufficiently mixed, a support is added to the solution and stirred to thoroughly contact the solution and support. The quantity of support is any amount sufficient to support the chromium pyrrolide compound. Generally, the amount of support necessary is the same as that disclosed in the previous exemplary process. Any suitable pressure and temperature can be used, although ambient temperature and pressure are preferred for ease of use. Usually, the mixing and/or contacting time is within the range of 30 minutes to one week, preferably from 3 hours to 48 hours. Most preferably, the mixing and/or contacting time is within the range of 5 hours to 24 hours, to maximize efficiency and result in a thoroughly contacted support. The solution then can be filtered to recover a solid catalytic product. The catalytic product, as with the reactants and reactions, is preferably kept under an inert atmosphere to maintain chemical stability. If the chromium compound is recovered and is to be used as an unsupported trimerization and/or polymerization catalyst, olefins can be trimerized or polymerized in a presence of one or more of the inventive homogeneous chromium compounds, an saturated hydrocarbon, and Lewis acid. Optionally, hydrogen can be added to the reactor to accelerate the reaction. Reactants Reactants applicable for use in polymerization with the catalyst and processes of this invention are olefinic compounds which can polymerize, i.e., react with the same or with other olefinic compounds. Catalyst of the invention can be used to polymerize at least one mono-1-olefin having from 2 to 30 carbon atoms, preferably from 2 to 8 carbon atoms. Exemplary compounds include, but are not limited to, ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, and mixtures thereof. A preferred reactant is ethylene, which is reacted according to the present invention to a polymer having a density in the range of 0.9 to 0.93 g/cc. Reactants applicable for use in the trimerization process, i.e., the combination of any three olefins, of this invention are olefinic compounds which can a) self-react, i.e., trimerize, to give useful products such as, for example, the self reaction of ethylene can give one hexene; and/or b) olefinic compounds which can react with other olefinic compounds, i.e., co-trimerize, to give useful products such as, for example, co-trimerization of ethylene plus hexene can give one decene and/or 1-tetradecene, co-trimerization of ethylene and 1-butane gives one octene, or 1-decene end ethylene con give 1-tetradecene and/or 1-docosene. As used herein, the term "trimerization" is intended to include "co-trimerization" as defined above. Suitable trimerizable olefinic compounds are those compounds having from 2 to 30 carbon atoms per molecule and having at least one olefinic double bond. Exemplary compounds include, but are not limited to acyclic and cyclic olefins such as, for example, ethylene, propylene, 1-butene, 2-butene, isobutylene, 1-pentene, 2-pentene, 1-hexene, 2-hexene, 3-hexene, 1-heptene, 2-heptene, 3-heptene, the four normal octenes, the four normal nonenes, and mixtures of any two or more thereof. If branched and/or cyclic olefins are used as reactants, while not wishing to be bound by theory, it is believed that steric hindrance could hinder tie trimerization process. Therefore, the branched and/or cyclic portion(s) of the olefin should be distant from the carbon-carbon double bond. Reaction Conditions The reaction products, i.e., trimers and/or polymers, can be prepared from the catalyst systems of this invention by solution reactions, slurry reactions, and/or gas phased reaction techniques using conventional equipment and contacting processes. Contacting of the monomer or monomers with the catalyst system can be effected by any manner known in the art of solid catalyst. One convenient method is to suspend the catalyst system in an organic medium and to agitate the mixture to maintain the catalyst system in suspension throughout the trimerization and/or polymerization process. Other known contacting methods such as fluidized bed, gravitating bed, and fixed bed can also be employed. Optionally, hydrogen can be added to the reactor to accelerate the reaction. The catalyst systems of this invention are particularly suitable for use in slurry trimerization and/or polymerizations. The slurry process is generally carried out in an inert diluent (medium), such as a paraffin, cycloparaffin, or aromatic hydrocarbon. One exemplary reactor diluent is isobutane. When the reactant is predominately ethylene, a temperature in the range of 60° to 110°C, preferably 66 to 110°C, is employed. Products The olefinic and/or polymeric products of this invention have established utility in a wide variety of application such as, for example, as monomers for use in the preparation of homopolymers, copolymers, and/or terpolymers. The polymeric products of this invention have established utility in a wide variety of application such as for example, polyethylene. The further understanding of the present invention and its advantages will be provided by reference to the following examples. Examples Preparation of Chromium-Containing Compounds Manipulations of all reactants were carried out either in a drybox employing nitrogen, or in airless glassware employing vacuum or nitrogen. Tetrahydrofuran (THF), toluene, benzene, diethylbenzene (Aldrich, 97% mixture of 1,2-, 1,3- 1,4- isomers) and pentane were purified by distillation over sodium benzophenone ketyl under nitrogen, then degassed via a nitrogen purge. Dimethoxyethane (DME) (Aldrich, anhydrous) was degassed via nitrogen purge and used without further purification. Pyrrole (Aldrich, 98%) was vacuum distilled over sodium, then degassed via nitrogen purge. 2,5-Dimethylpyrrole was dried with calcium sulfate and vacuum distilled. Sodium 2,5-dimethylpyrrolide (NaC₆H₈N) was prepared by reacting 2,5-dimethylpyrrole with an excess of sodium (40% by weight dispersion in mineral spirits) in refluxing tetrahydrofuran under nitrogen. Sodium pyrrolide was prepared by reacting pyrrole with an equivalent molar amount (1:1) of NaH (Aldrich, 60% by weight in mineral oil) or sodium (40% dispersion by weight in mineral spirits) in dimethoxyethane or tetrahydrofuran (THF) at ambient temperature under nitrogen. Triethylaluminum (TEA) (Aldrich 1.0M, hexanes and 1.9M Toluene) was used as received. Ketjen Grade B alumina (Al₂O₃) and Davison 952 silica (SiO₂) were the commercial materials used as supports for catalyst preparations. Fluorided-alumina (F/Al₂O₃, 15 wt% F) was prepared by the addition of a solution of NH₄HF₂ in methanol to Ketjen Grade B alumina. Phosphated silica (P/SiO₂, P/Si molar ratio = 0.1) was prepared by the addition of a 10% H₃PO₄/methanol solution to Davison 952 silica. The aluminophosphate (AlPO₄) used in the following experiments was made as described in McDaniel et al, U.S. Patent No. 4,364,855 (1982). The supports were activated by placing up to 25g into a fritted quartz tube, fluidizing with air and calcining at 700°C, except for P/SiO₂ at 350°C, for 3 hours. The air stream was switched to nitrogen until the support cooled to ambient temperature. Chromium pyrrolide complexes were typically prepared from anhydrous chromium (II or III) chloride and sodium pyrrolide as follows: A typical synthetic procedure useful to prepare chromium pyrrolide complexes was that of reacting the chromium chlorides with sodium pyrrolide (NaC₄H₄N, also referred to as NaPy) in refluxing tetrahydrofuran (THF). A molar reactant stoichiometry of 1CrCl₂ and 2NaPy resulted in the isolation of a polymeric material, Product II, as the major product, and a pentanuclear complex, Product I. (Cr₅(NC₄H₄)₁₀(OC₄H₈)₄), as the minor product, see Equation 1. Using molar excess of NaPy resulted in the isolation of the dianionic square planar complex {Cr(NC₄H₄)₄}{Na}₂·2OC₄H₈. Product III, and the octahedral complex {Cr(C₄H₄N)₅(OC₄H₈)}{Na}₂·4OC₄H₈, Product IV, see Equation 2. Each of the products was isolated through precipitation (Product II) or crystallization (Products I, III, IV) from THF solutions by the addition of pentane. Example I To prepare the pentanuclear complex, Product I, (Cr₅(NC₄H₄)₁₀(OC₄H₈)₄), and the polymeric material, Product II, chromous chloride (2.0g/16.3 mmole) was combined with sodium pyrrolide (33.7 mmole) in tetrahydrofuran and refluxed 20 hours. The reaction mixture was filtered (medium porosity frit) and the filtrate was used for fractional crystallization of both (Cr₅(NC₄H₄)₁₀(OC₄H₈)₄), Product I, and the polymeric material, Product II, through the addition of pentane. The polymeric material crystallized as a blue solid followed by (Cr₅(NC₄H₄)₁₀(OC₄H₈)₄) as opaque dark blue/purple crystals. Analysis calculated for C₅₆H₇₂N₁₀Cr₅O₄, ProductI:C, 55.62; H, 6.00; N, 11.58%, by weight. Found: C, 55.46; H, 6.32; N, 11.15%, by weight. Analysis found for Product II: Cr, 11.5; C, 59.75; H, 7.61; N, 9.17%, by weight, but variable upon precipitation conditions. An x-ray crystal structure of Product I showed a pentanuclear complex incorporating bridging amido-pyrrolyl, terminal amido-pyrrolyl, and tetrahydrofuran ligands (Figures 1 and 2). Example II To prepare {Cr(NC₄H₄)₄}{Na}₂·2OC₄H₈, Product III, and {Cr(C₄H₄N)₅(OC₄H₈)}{Na}₂·4OC₄H₈, Product IV, chromous chloride (3.0g/24.4mmole) was combined with sodium pyrrolide (100.9mmole) in tetrahydrofuran and refluxed 2 hours, see Equation 2. The reaction mixture was filtered (medium porosity frit) and the filtrate was used for fractional crystallization of both {Cr(NC₄H₄)₄}{Na}₂·2OC₄H₈, Product III, and {Cr(C₄H₄N)₅(OC₄H₈)}{Na}₂·4OC₄H₈, Product IV, through the addition of pentane. Product III crystallized as translucent orange/ red crystals followed by Product IV as translucent purple crystals. While not wishing to be bound by theory, the formation of Product IV is believed to result from the presence of chromic chloride in the chromous chloride reagent (Alfa, chromium (II) chloride, anhydrous, contains 5-10% by weight CrCl₃) used in the preparation. Analysis calculated for C₂₄H₃₂N₄O₂CrNa₂, Product III: C, 56.94: H, 6.32; N, 11.07% by weight. Found: C, 57.04; H, 6.30; N, 10.92%, by weight. Analysis calculated for C₄₀H₆₀N₅O₅CrNa₂, Product IV: C, 60.90; H, 7.67; N, 8.88% by weight. Found: C, 60.81; H, 7.74; N, 9.44%, by weight. An x-ray crystal structure of Product III showed a square planar complex incorporating terminal amido-pyrrolyl ligands (Figure 3). An x-ray crystal structure of Product IV showed an octahedral complex incorporating terminal amido-pyrrolyl and a tetrahydrofuran ligand (Figure 4). Example III The reaction product obtained from sodium pyrrolide end CrCl₃ was the most preferred in the preparation of an active catalyst. Pyrrole (7.0ml/100.9mmole) was mixed with NaH (4.2g of 60%, ∼ 105 mmole) in dimethoxyethane at ambient temperature until bubbling ceased. Chromic chloride (5.33g/33.7mmole) was added to the solution at ambient temperature. The reaction mixture was refluxed under nitrogen for five hours, see Equation 3. This resulted in a dark green solution. The solution was filtered (medium porosity frit) and stripped of solvent under vacuum and pumped dry under vacuum for 12 hours. The resultant chromium pyrrolide complex was a green solid, Product V. It was used in the preparation of an active catalyst without further purification. All single crystal x-ray structure analyses were performed by Crystalytics Company, Lincoln, Nebraska. Examples IV, V, and VI contain the resultant analytical and subsequently computer-generated data. A single crystal x-ray structure was obtained for [Cr₅(NC₄H₄)₁₀(OC₄H₈)₄], Product I, and shown in Figure I and Figure II. The description of the single-crystal sample and mounting used for data collection are as follows: Color: Dark blue Shape: Rectangular parallelepiped Dimensions: 0.20 x 0.48 x 0.80 mm Crystal Mount: Crystal was sealed inside a thin-walled glass capillary with epoxy under N₂. Crystal Orientation: Crystal was oriented with its longest edge nearly parallel to the phi axis of the diffractometer. Width at Half-height from W Scans: 0-38° The space group and cell data are as follows: Crystal System: Triclinic Space Group and Number: Pl-C i (No. 2) Number of Computer-Centered Reflections Used in the Least-Squares Refinement of the Cell Dimensions: 15 2ϑ>25° °C=20±1° Lattice Constants with esd's: a = 10.803(2)Å α = 85.59(2)° V = 1407.9(6)Å b = 9.825(2)Å β = 96.23(2)° Z = 1 c = 14.212(4)Å γ = 109.99(2)° τ* = 0.71073Å Molecular Weight: 1209.24 amu Calculated Density: 1.427 g/cc Linear Absorption Coefficient: 0.96 mm⁻¹ Tables I - V list the resultant parameters used to generate the molecular structure shown in Figure I and Figure II. Example V A single crystal x-ray structure was obtained for Cr(NC₄H₄)₄, a portion of Product III and shown in Figure III. A single crystal x-ray Structure was obtained for [Na]₂[Cr(NC₄H₄)₄]2(OC₄H₈), Product III and shown in Figure IV. The description of the single-crystal sample and mounting used for the data collection are as follows: Color: Red-orange Shape: Rectangular parallelepiped Dimensions: 0.50 x 0.55 x 0.65 mm Crystal Mount: Crystal was glued to the inside of a thin-walled glass capillary and sealed under N₂. Crystal Orientation: Crystal was oriented with its longest edge nearly parallel to the phi axis of the diffractometer. Width at Half-height from W Scans: 0.86° The space group and cell data are as follows: Crystal System: Monoclinic Space Group and Number: C2/c - C 2h(No. 15) Number of Computer-Centered Reflections Used in the Least-Squares Refinement of the Cell Dimensions: 15 2ϑ>25° °C = 20±1° Lattice Constants with esd's: a = 9.522(2)Å α = 90.00° V = 2697(1)Å b = 15.118(2)Å β = 98.99(1)° Z = 4 c = 18.967(3)Å γ = 90.00° τ = 0.71073Å Molecular Weight: 506.52 amu Calculated Density: 1.248 g/cc Linear Absorption Coefficient: 0.47mm⁻¹ Tables VI-X list the resultant parameters used to generate the molecular structure shown in Figure III and Figure IV. Atomic Coordinates for Nonhydrogen Atoms in Crystalline {Na}₂{Cr(NC₄H₄)₄} - 2 OC₄H₈ Atom Type Fractional Coordinates Equivalent Isotropic Thermal Parameter, B, Å² x 10 10⁴x 10⁴y 10⁴x Anion Cr ⊘ 2982(1) 25⊘⊘ d 5⊘(1) N₁ 19⊘1(4) 2924(2) 3183(2) 56(1) N₂ ⊘ 4343(3) 25⊘⊘ d 52(1) N₃ ⊘ 1612(3) 25⊘⊘ d 7⊘(2) C₁₁ 3241(5) 295⊘(3) 3⊘⊘8(3) 65(2) C₁₂ 4224(6) 2768(3) 3587(3) 73(2) C₁₃ 3513(7) 263⊘(4) 4146(3) 82(2) C₁₄ 2⊘94(7) 2734(4) 3884(3) 76(2) C₂₁ 9⊘7(5) 4884(3) 2926(3) 6⊘(1) C₂₂ 582(4) 5753(3) 2766(3) 69(2) C₃₁ 39⊘(5) 1⊘81(3) 1996(4) 94(2) C₃₂ 236(7) 213(3) 2189(5) 133(6) Cation Na 23⊘1(2) 6⊘79(1) 1783(1) 69(1) Solvent of Crystallization O₁ 2⊘65(4) 51⊘8(2) 83⊘(2) 83(1) C₄₁ 2759(11) 5174(5) 239(4) 143(4) C₄₂ 28⊘4(11) 4319(5) -79(4) 148(4) C₄₃ 1893(1⊘) 3786(5) 264(5) 142(4) C₄₄ 1699(9) 4231(4) 9⊘2(4) 12⊘(3) Anisotropic Thermal Parameters for Nonhydrogen Atoms in Crystalline {Na}₂{Cr(NC₄H₄)₄} - 2 OC₄H₈ , Atom Type Anisotropic Thermal Parameter (Å² x 10) B₁₁ B₂₂ B₃₃ B₁₂ B₁₃ B₂₃ Anion Cr 64(1) 34(1) 55(1) ⊘ d 15(1) ⊘ N₁ 69(2) 44(2) 56(2) 6(1) 12(1) 6(1) N₂ 64(3) 39(2) 56(3) ⊘ d 16(2) ⊘ d N₃ 65(3) 38(2) 1⊘7(4) ⊘ d 14(3) ⊘ d C₁₁ 78(3) 5⊘(2) 7⊘(3) -6(2) 18(2) 2(2) C₁₂ 7⊘(3) 62(3) 84(3) 4(2) 7(2) -8(2) C₁₃ 1⊘3(4) 79(3) 58(3) 22(3) -8(3) ⊘(2) C₁₄ 86(3) 86(3) 58(3) 16(3) 16(2) 5(2) C₂₁ 66(2) 45(2) 7⊘(3) -2(2) 15(2) -6(2) C₂₂ 68(3) 38(2) 1⊘5(4) -7(2) 27(2) -9(2) C₃₁ 65(3) 61(3) 152(5) 6(2) 9(3) -36(3) C₃₂ 71(5) 46(2) 266(15) 6(3) -28(6) -44(4) Cation Na 7⊘(1) 57(1) 81(1) -2(1) 15(1) -15(1) Solvent of Crystallization O₁ 1⊘8(2) 65(2) 82(2) -1⊘(2) 38(2) -16(2) C₄₁ 222(8) 112(5) 116(5) -46(5) 92(6) -22(4) C₄₂ 192(8) 16⊘(8) 1⊘7(5) 12(6) 7⊘(5) -32(5) C₄₃ 147(6) 1⊘9(6) 177(8) -27(5) 48(6) -69(6) C₄₄ 177(6) 77(4) 124(5) -21(4) 76(5) -14(3) Anion Bond Lengths and Bond Angles Involving Nonhydrogen Atoms in Crystalline {Na}₂{Cr(NC₄H₄)₄} - 2 OC₄H₈ Type Length, Å Type Length, Å Cr-N₁ 2.057(3) C₁₁-C₁₂ 1.355(7) Cr-N₂ 2.056(4) C₁₂-C₁₃ 1.361(9) Cr-N₃ 2.072(5) C₁₃-C₁₄ 1.374(9) C₂₁-C₂₂ 1.372(6) N₁-C₁₁ 1.369(7) C₂₂-C 22' 1.379(9) N₁-C₁₄ 1.344(6) C₃₁-C₃₂ 1.376(7) N₂-C₂₁ 1.360(5) C₃₂-C 32' 1.327(18) N₃-C₃₁ 1.344(7) Type Angle, deg. Type Angle, deg. N₁CrN₂ 92.5(1) N₁C₁₁C₁₂ 110.5(5) N₁CrN₃ 87.5(1) C₁₁C₁₂C₁₃ 107.3(5) N₁CrN 1' c 175.1(2) C₁₂C₁₃C₁₄ 106.4(5) N₂CrN₃ 180.0(-) d N₁C₁₄C₁₃ 110.9(5) N₂C₂₁C₂₂ 110.2(4) CrN₁C₁₁ 127.5(3) C₂₁C₂₂C 22' 106.8(3) CrN₁C₁₄ 127.1(4) N₃C₃₁C₃₂ 109.1(6) C₁₁N₁C₁₄ 104.9(4) C₃₁C₃₂C 32' 107.5(5) CrN₂C₂₁ 127.0(2) C₂₁N₂C 21' 106.0(5) CrN₃C₃₁ 126.7(3) C₃₁N₃C 31' 106.7(6) Bond Lengths and Angles Involving the Nonhydrogen Atoms of the Cation and Solvent of Crystallization in {Na}₂{Cr(NC₄H₄)₄} - 2 OC₄H₈ Type Length, Å Type Length, Å Na-O₁ 2.313(4) O₁-C₄₁ 1.390(10) O₁-C₄₄ 1.382(7) Na···N 1'' c 2.888(4) Na···N 3'' c 2.830(4) C₄₁-C₄₂ 1.43(1) C₄₂-C₄₃ 1.42(1) C₄₃-C₄₄ 1.42(1) Type Angle, deg. Type Angle, deg. O₁NaN 1'' 128.6(3) C₄₁O₁C₄₄ 107.9(5) O₁NaN 3'' 121.8(3) N 1'' NaN 3'' 59.9(3) O₁C₄₁C₄₂ 109.0(7) C₄₁C₄₂C₄₃ 105.0(8) NaO₁C₄₁ 125.7(4) C₄₂C₄₃C₄₄ 107.0(7) NaO₁C₄₄ 121.8(4) O₁C₄₄C₄₃ 107.6(7) Example VI Single crystal x-ray structures were obtained for [Cr(NC₄H₄)₅(OC₄H₈)], shown in Figure V, + [Cr(NC₄H₄)₅(OC₄H₈)][Na]₂ - 4(OC₄H₈), Product IV, + shown in Figure VI. The description of the single-crystal sample and mounting used for data collection are as follows: Color: Purple Shape: Rectangular parallelepiped Dimensions: 0.50 x 0.55 x 0.63 mm Crystal Mount: Crystal was glued to the inside of a thin-walled glass capillary and sealed under N₂. Crystal Orientation: Crystal was oriented with its longest edge nearly parallel to the phi axis of the diffractometer. Width at Half-height from W Scans: 0.42° The space group and cell data are as follows: Crystal System: Monoclinic Space Group and Number: P2₁-C₂²(No. 4) Number of Computer-Centered Reflections Used in the Least-Squares Refinement of the Cell Dimensions: 15 2ϑ>20° °C=20±1° Lattice Constants with esd's: a = 10.042(2)Å α = 90.00° V = 2162(1)Å b = 17.242(4)Å β = 106.54(2)° Z = 2 c = 13.025(3)Å γ = 90.00° τ = 0.71073Å Molecular Weight = 788.93 amu Calculated Density: 1.212 g/cc Linear Absorption Coefficient: 0.32 mm⁻¹ Tables XI - XV list the resultant parameters used to generate the molecular structure shown in Figure V and Figure VI. Example VII The product obtained from the reaction of sodium 2,5-dimethylpyrrolide and CrCl₂ used in the preparation of an active catalyst was a light blue solid, Product VI. 2,5-Dimethylpyrrole (5.0ml/49.1mmole) was mixed with excess sodium (40% dispersion in mineral spirits) in tetrahydrofuran (125ml) at ambient temperature. The mixture was refluxed 12 hours under nitrogen then filtered to remove excess sodium. The sodium 2,5-dimethylpyrrolide was used in-situ and combined with chromous chloride (3.03g/24.7mmole) at ambient temperature. The reaction mixture was refluxed under nitrogen for 48 hours. The gray-green solution was filtered (medium porosity frit) at ambient temperature and stripped of solvent under vacuum, then pumped dry under vacuum for 12 hours resulting in a gray/green solid. This grey/green solid was then washed with pentane resulting in a light blue solid, Product VI, which was collected by filtration. Product VI was used in the preparation of an active catalyst without further purification. Example VIII All polymerization runs were carried out in a two liter reactor under slurry (particle form) conditions. The diluent was isobutane and the reactor temperature was 90°C. Reactor pressure held at 3900 kPa (550 psig) during the polymerization, with ethylene being fed on demand. The actual charging of the reactor was accomplished by the following method. After purging the reactor at 100°C with a stream of nitrogen for at least 15 minutes, the reactor temperature was lowered to 90°C and a preweighed amount of supported chromium pyrrolide catalyst was charged against a slight countercurrent of nitrogen. One liter of isobutane was then charged to the reactor and finally the reactor pressurized with ethylene. The ethylene consumed was determined using a precalibrated ethylene flow meter. Samples of the liquid product mixture were taken after 30 minute run time without depressurizing the reactor. This was done by filling to 1480-2170 kPa (200-300 psig) a steel sampling cylinder adapted to the reactor with a dip tube fitted with a fritted tip extending into the bottom of the reactor vessel. Samples taken this way were analyzed by gas chromatography and gas chromatography-mass spectrometry. Selectivities were normalized to 100%. Solid products were obtained by venting the reactor to atmosphere, separating by decantation of the liquids from the solid material. The solids were then dried at 100°C in a vacuum oven and weighed. The yield of solid product was obtained by weighing the combined solid and catalyst residues and subtracting from this the preweighed catalyst charge. The yield of volatile products was obtained by subtracting the yield of solid products from the grams of ethylene consumed as recorded by the flow meter. Activity typically ranged from 300-1500 g product/g catalyst/hour calculated for 30 minute run time, as shown in Table XVI. The product obtained typically was represented by 97-99.5% by weight liquids and 0.5-3% by weight polymer (wax). The liquid fraction was typically 85% hexenes, 11% decenes, 2% tetradecenes, based on the total weight of the liquid fraction. The balance of the liquid product mixture was a trace level distribution of olefins typically totalling about 1-2% by weight of the product mixture, see Table XVII. Active catalysts were prepared from the chromium pyrrolide complexes as follows. All toluene and/or pentane rinses used 15 to 30mls of liquid. 0.158g of Product V (prepared in THF solvent), which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml toluene at ambient temperature. 9.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (2.00g) was added to the solution and stirred for an additional 24 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.3143g of the catalyst was charged directly to the reactor for polymerization. 1.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 2: 0.081g of Product V (prepared in THF solvent), which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml diethylbenzene at ambient temperature. 2.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (1.50g) was added to the solution and stirred for an additional 1 hour. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with dimethylbenzene, and then twice with pentane. 0.4333g of the catalyst was charged directly to the reactor for polymerization. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 3: 0.093g of Product V (prepared in DME solvent) was slurried with 15ml toluene at ambient temperature. 5.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (1.0g) was added to the solution and stirred for an additional 24 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.1564g of the catalyst was charged directly to the reactor for polymerization. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. 0.080g of Product I (prepared in THF solvent) was slurried with 15ml toluene at ambient temperature. 6.0ml of a 1M TEA in hexanes solution was added and the solution stirred for 16 hours. The formation of a brown solution and the complete dissolution of Product I resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (1.50g) was added to the solution and stirred for an additional 16 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice pentane 1.1988g of the catalyst was charged directly to the reactor for polymerization. Run 5: 0.079g of Product II (prepared in THF solvent) was slurried with 15ml toluene at ambient temperature. 2.0ml of a 1.9M TEA in toluene solution was added to the solution and stirred for 8 hours. The formation of a brown solution and the complete dissolution of Product II resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (0.50g) was added to the solution and stirred for an additional 16 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then tiwce with pentane. 0.4829g of the catalyst was charged directly to the reactor for polymerization. Run 6: 0.071g of Product V (prepared in THF solvent), which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml toluene at ambient temperature. 2.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 1 hour. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. SiO₂(2.52g) was added to the solution and stirred for an additional 2 minutes. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. Run 7: 0.103g of Product II (prepared in THF solvent) was slurried with 15ml toluene at ambient temperature. 1.0ml of a 1.9M TEA in toluene solution was added to the solution and stirred for 10 minutes. The formation of a brown solution and the complete dissolution of Product II resulted immediately upon TEA addition. A1203 (2.27g) was added to the solution and stirred for an additional 2 minutes. The supported catalsyt was filtered from the solution as a brown solid. rinsed twice with toluene, and then twice with pentane. 1.2926g of the catalyst was charged directly to the reactor for polymerization. Run 8: 0.120g of Product I (prepared in THF solvent) was slurried with 15ml toluene at ambient temperature. 2.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 2 days. The formation of a brown solution and the complete dissolution of Product I resulted immediately upon TEA addition. SiO₂(1.0g) was added to the solution and stirred for an additional 3 weeks. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. Run 9: 0.106g of Product III (prepared in THF solvent) was slurried with 15ml toluene at ambient temperature. 2.5ml of a 1.9M TEA in toluene solution was added to the solution and stirred for 2 hours. The formation of a brown solution and the complete dissolution of Product III resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (0.65g) was added to the solution and stirred for an additional 2 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. 1.5ml of a 1.0% TEA in pentane solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 10: 0.030g of Product V (prepared in THF solvent) which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF was slurried with 15ml toluene at ambient temperature. 3.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 16 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al = .9) (2.0g) was added to the solution and stirred for an additional 16 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.322/g of catalyst was charged directly to the reactor for polymerization. Run 11: 0.067g of Product V (prepared in THF solvent) was slurried with 15ml pentane at ambient temperature. 4.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (1.0g) was added to the solution and stirred for an additional 24 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 12: 0.073g of Product V (prepared in THF solvent), which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml toluene at ambient temperature. 6.0ml of a 1M TEA in hexanes solution was added and the solution stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. P/SiO₂ (7.0g) was added to the solution and stirred for an additional 24 hours which nearly decolorized it. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 2.85g of catalyst was charged directly to the reactor for polymerization. Run 13: 0.125g of Product II was slurried with 15ml diethylbenzene at ambient temperature. 9.0ml of a 1M TEA in hexanes solution was added to the solution and stirred for 8 hours. The formation of a brown solution and the complete dissolution of Product II resulted immediately upon TEA addition. P/Al₂O₃ (2.0g) was added to the solution and stirred for an additional 12 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.5477g of catalyst was charged directly to the reactor for polymerization. Run 14: 0.125g of Product VI was slurried with 15ml toluene at ambient temperature. 1.5ml of a 1M TEA in hexanes solution was added and the solution stirred for 10 minutes. The formation of a red/brown solution and the complete dissolution of Product VI resulted immediately upon TEA addition. SiO₂ (2.0g) was added to the solution and stirred for an additional 1 minute which nearly decolorized it. The supported silica catalyst was filtered from the solution as a red/brown solid. rinsed twice with toluene, and then twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. Run 15: 0.30g of Product V (prepared in DME solvent) was dissolved with 15ml of dimethoxyethane forming a green solution. This solution was then mixed with 0.6g of AlPO₄(P/Al₄ mole ratio = 0.4) (2.00g) and the mixture was stirred 1 hour. The green supported material was filtered from the solution, rinsed with dimethoxyethane and dried with a nitrogen purge at 90°C. This material was then stirred with 15ml of toluene and 3ml of triethylaluminum (Aldrich 1.0M, hexanes) for an additional 3 hours. The brown supported catalyst was collected by filtration, rinsed with pentane, and dried under vacuum. 0.4609g of the catalyst was charged directly to the reactor for polymerization. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 16: 0.058g of Product V (prepared in THF solvent) which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF was slurried with 15ml benzene at ambient temperature. 4.0ml of a 1M TEA in hexanes solution was added and the solution stirred for 2 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. AlPO₄(P/Al mole ratio = 0.4) (1.0g) was added to the solution and stirred for 1 hour. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with benzene, and then twice with pentane. All of the catalyst was charged directly to the reactor for polymerization. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge but before the isobutane (reactor solvent) charge to purge feedstock poisons. Run 17: 0.1610g of Product I was charged directly to the reactor at 90°C. The reactor was charged with 1 liter isobutane and pressurized to 3900 kPa (550 psig) with ethylene. No ethylene consumption was detected, therefore 450 kPa (50 psig) of dihydrogen was charged to the reactor which did not initiate ethylene consumption. Ethylene consumption was initiated after 2.0ml of 1M TEA in hexanes solution was charged. Run 18: 0.3528g of Product VI was charged directly to the reactor at 90°C. The reactor was charged with 1 liter isobutane and pressurized to 3900 kPa (550 psig) with ethylene. No ethylene consumption was detected, therefore 2.0ml of a 1M TEA in hexanes solution was charged which did initiate ethylene consumption. Run 19: 0.3482g of Product VI was charged directly to the reactor at 90°C. The reactor was also charged with 2.0ml of a 1M TEA in hexanes solution prior to a 1 liter isobutane charge. The reactor was then pressurized to 3900 kPa (550 psig) with ethylene. No ethylene consumption was detected, therefore 310 kPa (30 psi) of dihydrogen was charged to the reactor which initiated ethylene consumption. The data in Table XVI show that the inventive chromium compounds can be used either supported (Runs 1-16) or unsupported (Runs 17-19) to polymerize and/or trimerize olefins. Furthermore, conditions can be varied to increase the amount of trimer product (Runs 1-5 and 9) or to have a higher yield of solid, or polymer, product (Runs 6, 7, and 13). Runs 1 and 3 demonstrate that high activities are attainable. Example IX All polymerization runs were carried out as described in Example VIII. Density was determined in grams per cubic centimeter (g/cc) on a compression molded sample, cooled at 15°C per hour, and conditioned for 40 hours at room temperature in accordance with ASTM D1505 and ASTM D1928, condition C. The high load melt index (HLMI) was determined in accordance with ASTM D1238 at 190°C with a 21,600 gram weight. Melt index (MI) was determined according to ASTM D1238 at 190°C with a 2,160 gram weight. Run 20 : 0.100g of Product V (prepared in THF solvent), which was heated to 80 C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml toluene at ambient temperature. 7.0ml of a 1M TEA in hexanes solution was added and the solution stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. An AlPO₄ (P/Al mole ratio = 0.4) (2.0g) was added to the solution and stirred for 2 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.225g of this catalyst was mixed with 0.078g of a tergel-supported chromium catalyst as two free-flowing powders. The tergel-supported chromium catalyst was prepared in accordance with procedures in U.S. Patent 3,887,494. 0.2576g of this catalyst mixture was charged directly to the polymerization reactor. 3.0ml of a 0.5% TEA in heptanes solution was charged to the reactor after the catalyst charge, but before the isobutane (reactor solvent) charge, to purge feedstock poisons. The reactor was pressurized to 3900 kPa (550 psig) with ethylene. After a 60.8 minute run time, 190g of polymer was produced. The polymer had a MI = 6.5, HLMI = 366.2, and a denstiy equal to 0.0132 g/cc. The catalyst activity was 730 g polymer/g catalyst/hr based on a 60.8 minute run time (run temperature 90°C, 3900 kPa (550 psig) total pressure). Run 21 : 0.100g of Product V (prepared in THF solvent), which was heated to 80°C for 4 hours under nitrogen flush to remove residual THF, was slurried with 15ml toluene at ambient temperature. 7.0ml of a 1M TEA in hexanes solution was added and the solution stirred for 24 hours. The formation of a brown solution and the complete dissolution of Product V resulted immediately upon TEA addition. An AlPO₄ support (P/Al mole ratio = 0.4) (2.0g) was added to the solution and stirred for 2 hours. The supported catalyst was filtered from the solution as a brown solid, rinsed twice with toluene, and then twice with pentane. 0.2314g of this catalyst was mixed with 0.0184g of a titanium-containing catalyst as two free-flowing powders. The titanium-containing catalyst was prepared in accordance with procedures in U.S. Patents 4,325,837 and U.S. 4,326,988 wherein ethylaluminumdichloride was the aluminum alkyl used. 0.2385g of this catalyst mixture was charged directly to the polymerization reactor. 3.0ml of a 0.5 percent TEA in heptanes solution was charged to the reactor after the catalyst charge, but before the isobutane (1 liter, the reactor solvent) charge, to purge feedstock poisons. 450 kPa 50 psig of dihydrogen (H₂) was then charged to the reactor, followed by pressurizing to 3900 kPa (550 psig) with ethylene. After a 31.0 minute run time, 82g of polymer was produced. The polymer had a MI=0.011, HLMI=0.63, and a density equal to 0.9429 g/cc. The catalyst activity was 670g polymer/g catalyst/hr based on a 31.0 minute run time (run temp. 90°C, 3900 kPa (550 psig) total pressure). While this invention has been described in detail for the purpose of illustration, it is not to be construed as limited thereby but is intended to cover all changes and modifications within the spirit and scope thereof.

Claims: A process for polymerizing olefins in the presence of a polymerization catalyst and a cocatalyst, characterized by said cocatalyst having been prepared by reacting a mixture of a chromium salt, a metal amide and an ether. The process of claim 1 wherein said polymerization catalyst is a supported chromium catalyst. The process of claim 1 wherein said polymerization catalyst is a titanium-containing catalyst. The process of any of the preceding claims wherein said cocatalyst is a chromium compound selected from Cr₅(C₄H₄N)₁₀(C₄H₈O)₄; Cr(C₄H₄N)₄; [Cr(C₄H₄N)₄][Na]₂x2(OC₄H₈); [Cr(C₄H₄N)₅(OC₄H₈)]; [Cr(C₄H₄N)₅(OC₄H₈)][Na]₂x4(OC₄H₈); and mixtures thereof. The process of any of the preceding claims wherein said cocatalyst is supported on an inorganic oxide. The process of any of the preceding claims wherein said olefin has from 2 to 30 carbon atoms. The process of claim 6 wherein said olefin is selected from ethylene, propylene, 1-butene, 1-hexene, and mixtures thereof. The process of claim 7 wherein said olefin is predominantly ethylene. The process of any of the preceding claims wherein said polymerization is carried out at a temperature within the range of 66 to 110 °C. The process of any of the preceding claims wherein hydrogen is present during said polymerization. The process of any of the preceding claims being carried out as slurry polymerization. The process of any of the preceding claims wherein said olefin is ethylene and the recovered polymer has a density within the range of 0.9 to 0. 93 g/ml.

Inventors: REAGEN WILLIAM KEVIN, REAGEN, WILLIAM KEVIN
Applicants: PHILLIPS PETROLEUM CO, PHILLIPS PETROLEUM COMPANY
Application year: 1990
Main classification: C08F4
IPC codes: C08F10, C08F4, C07C2, C08F210, C08F110