LOW PRESSURE PREPARATION OF ETHYLENE COPOLYMERS IN FLUID BED REACTOR

Abstract: Ethylene copolymers having a density of ≧ 0.91 to ≦ 0.96 and a melt flow ratio of ≧ 22 to ≦ 32 are readily produced in a low pressure gas phase process at a productivity of ≧ 50,000 pounds of polymer per pound of Ti with a particulate catalyst diluted with an inert carrier material and formed from selected organo aluminum compounds and a precursor composition of the formula: Mg m Ti₁(OR) n X p [ED] q wherein ED is a selected electron donor compound. m is ≧ 0.5 to ≦ 56 n is 0 or 1 p is ≧ 6 to ≦ 116 q is ≧ 2 to ≦ 85 R is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, or COR′ wherein R′ is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, and X is selected from the group consisting of Cl, Br, l or mixtures thereof. This application is a Continuation-in-Part of co-pending application Serial No. 892,325 filed March 31, 1978.

Description: The invention relates to a process of copolymerizing ethylene with one or more higher α-olefin monomers employing high activity Mg and Ti containing complex catalysts in a low pressure gas phase fluid bed process to produce polymers having a density of ≧ 0.91 to ≦ 0.96 g/cm³ and a melt flow ratio of ≧ 22 to ≧ 32. Until recently, low density (≦ 0.940 g/cm³) polyethylene has been produced commercially, for the most part, by the high pressure ≧ 1050 bar (≧ 10,000 psi) homopolymerization of ethylene in the gas phase in stirred and elongated tubular reactors in the absence of solvents using free radical initiators. On a world wide basis, the amount of low density polyethylene produced in this fashion, annually, amounts to more than about 6.10⁶ billion kg. As recently disclosed in US-A-4 011 382 and in BE-A-839 380 it has been found that low density polyethylene can be produced commercially at pressures of < 69 bar (< 1000 psi) in a gas phase reaction in the absence of solvents by employing selected chromium and titanium (and, optionally, fluorine) containing catalysts under specific operating conditions in a fluid bed process. The products produced by the processes of US-A-4 011 382 and BE-A-839 380, however, have a relatively broad molecular weight distribution (Mw/Mn) of ≧ 6 to ≦ 20. As such, although readily useful for a large number of applications in the areas of wire and cable insulation and molded pipe, they are not broadly useful in the area of injection molding applications. They are also not broadly used in the area of film applications because of the poor optical and mechanical properties of films made from such resins. To be commercially useful in a gas phase process, such as the fluid bed processes of US-A-3 709 853, 4 003 712 and 4 011 382 and CA-A-991 798 and BE-A-839 380, the catalyst employed must be a high activity catalyst, that is, it must have a level of productivity of ≧ 50,000, and preferably ≧ 100,000 kg of polymer per kg or primary metal in the catalyst. This is so because such gas phase processes usually do not employ any catalyst residue removing procedures. Thus, the catalyst residue in the polymer must be so small that it can be left in the polymer without causing any undue problems in the hands of the resin fabricator and/or ultimate consumer. Where a high activity catalyst is successfully used in such fluid bed processes, the primary metal content of the resin is of the order of ≦ 20 parts per million (ppm) at a productivity level of ≧ 50,000 and of the order of ≦ 10 ppm at a productivity level of 100,000 kg of polymer per kg of primary metal, and of the order of ≦ 3 ppm at a productivity level of ≧ 300,000 kg of polymer per kg of primary metal. Low catalyst residue contents are also important where the catalyst is made with chlorine containing materials such as the titanium, magnesium and/or aluminum chlorides used in some so-called Ziegler or Ziegler-Natta catalysts. High residual chlorine values in a molding resin will cause pitting and corrosion on the metal surfaces of the molding devices. Cl residues of the order of ≧ 200 ppm are not commercially useful. US-A-3 989 881 discloses the use of a high activity catalyst for the manufacture, under slurry polymerization conditions, of ethylene polymers having a relatively narrow molecular weight distribution (Mw/Mn) of about 2.7 to 3.1. Attempts were made to use catalysts similar to those described in US-A-3 989 881 for the purpose of making polyethylene of narrow molecular weight distribution of polymerizing ethylene alone, or with propylene, and in the gas phase in a fluid bed process using apparatus and conditions similar to those employed in US-A-4 011 382 and BE-A-839 380. These attempts were not successful. In order to avoid the use of the solvents in the slurried catalyst systems of US-A-3 989 881, the Ti/Mg containing components were dried. However, the dried material a viscous, gummy, phyrophoric composition, could not be readily fed to the reactor because it was not in a free flowing form. Even when blended with silica, to improve its free flowing properties, and then added to the reactor the results were commercially unacceptable. The productivity of the catalyst was poor, or the catalyst was pyrophoric and difficult to handle, or the polymer product had a low bulk density, i.e. of the order of ≦ 0.1 g/cm³ (≦ 6 pounds/cubic foot) at a density of ≦ 0.940 g/cm³. Materials having such a low bulk density cannot be fluidized in a fluid bed process under acceptable operating conditions. Polymers of such low bulk density are also not commercially desirable because they are fluffy. If the polymer is to be stored or sold in granular form, significantly larger amounts of storage and shipping space is required for handling these materials. Even if the granular polymer is to be pelletized prior to shipping, the processing of a given quantity of the low bulk density material through the pelletizing equipment requires significantly longer processing times than would the same quantity of high bulk density materials, when using the same extrusion equipments. US-A-4124 532 discloses the polymerization of ethylene and propylene with high activity catalysts. These catalysts comprise complexes which may contain magnesium and titanium. These complexes are prepared by reacting the halide MX₂ (where M may be Mg) with a compound M′Y (where M′ may be Ti and Y is halogen or an organic radical) in an electron donor compound. These complexes are then isolated by either crystallization, by evaporation of the solvent or by precipitation. Polymerization is carried out with these complexes and an alkyl aluminum compound. However, US-A-4 124 532 does not disclose any special techniques or methods or preparing the catalyst in order to achieve the desirable results described in the present invention. The use of the catalysts described in US-A-4124 532, without these special methods, would not lead to a commercial fluid bed process to produce polyethylenes at commercial rates. Thus, even when diluted with a carrier and employed in a fluid bed process, it has been found that polymerization cannot be sustained on a continuous basis with such catalysts. The reason for this is that the catalysts are needle-like in shape and when activated in a fluid bed produce polymers which also have a needle-like shape. The production of such needle-shaped polymers soon causes a termination of fluidization in the bed and a cessation of polymerization. In addition, the examples of gas phase polymerization in this patent do not illustrate copolymerization to produce high density polyethylene copolymer, let alone a practical process for producing the special low density copolymers described in our present invention. US-A-3 922 322 and 4 035 560 disclose the use of several Ti and Mg containing catalysts for the manufacture of granular ethylene polymers in a gas phase fluid bed process under a pressure of < 69 bar (< 1000 psi). The use of these catalysts in these processes, however, has significant disadvantages. The catalysts of US-A-3 922 322 provide polymers having a very high catalyst residue content, i.e., about 100 ppm of Ti and greater than about 300 ppm Cl, according to the working example of this patent. Further, as disclosed in the working example of US-A-3 922 322, the catalyst is used in the form of a prepolymer, and very high volumes of the catalyst composition must be fed to the reactor. The preparation and use of this catalyst thus requires the use of relatively large sized equipment for the manufacture, storage and transporting of the catalyst. The catalysts of US-A-4 035 560 also apparently provide polymers having high catalyst residues, and the catalyst compositions are apparently pyrophoric because of the types and amounts of reducing agents employed in such catalysts. It has now been unexpectedly found that ethylene copolymers having a wide density range of 0.91 to 0.96 g/cm³ and a melt flow ratio of ≧ 22 to ≦ 32, and which have a relatively low residual catalyst content, can be produced at relatively high productivities for commercial purposes by a gas phase fluid bed process if the ethylene is copolymerized with one or more C₃ to C₈ α-olefins in the presence of a high activity magnesium-titanium complex catalyst prepared, as described below, under specific activation conditions with an organo aluminum compound and an inert carrier material. An object of the present invention is to provide a process for producing, at relatively high productivities and in a low pressure gas phase fluid bed process, ethylene copolymers which have a density of 0.91 to 0.96 g/cm³, a melt flow ratio of ≧ 22 to ≦ 32 and a relatively low residual catalyst content. A further object of the present invention is to provide a process in which ethylene copolymers, which are useful for a variety of end-use applications, may be readily prepared. The new process for copolymerizing ethylene employs a catalyst composition prepare By forming a precursor composition from a magnesium compound, titanium compound and electron donor compound, and then activating the precursor composition with an organoaluminum compound to form the catalyst, which is characterized in that the polymerization is conducted continuously in a fluid bed reactor at a temperature of from 30 to 115°C under a pressure of < 69 bar (< 1000 psi) in the gas phase by contacting a mixture of ethylene and one or more C₃ to C₈ α-olefin monomers, said mixture containing from 0 to 2.0 moles of hydrogen per mol of ethylene, with particles of an activated precursor composition wherein said precursor composition has the formula Mg m Ti(OR) n X p [ED] q wherein m is ≧ 1.5 to ≦ 56 n is 0 or 1 p is ≧ 6 to ≦ 116 q is ≧ 2 to ≦ 85 R is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, or COR′ wherein R′is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, X is selected from the group consisting of Cl, Br, l or mixtures thereof; ED is a liquid organic electron donor compound in which said precursor composition and the Ti and Mg components thereof are partially or completely soluble and which is selected from the group consisting of alkyl esters of aliphatic and aromatic carboxylic acids, aliphatic ethers, cyclic ethers and aliphatic ketones, said precursor composition having an average particle size of 10 to 100 µm, a bulk density of 0.289 to 0.529 g/cm³ (18 to 33 pounds per cubic foot), and being mechanically mixed or blended with at least one solid inert carrier material in a ratio of 0.033 to 1 part of precursor composition per part by weight of carrier material, said carrier material being optionally pretreated with about 1 to 8 weight percent of one or more aluminum alkyl compounds, and being activated with an activator compound having the formula Al(R″) c X′ d H e wherein X′ is Cl or OR‴, R″ and R‴ are the same or different and are C₁ to C₁₄ saturated hydrocarbon radicals, d is 0 to 1.5, e is 0 or 1, and c + d + e = 3 activation of said precursor composition being effected by treating said precursor composition outside the polymerization reactor in a hydrocarbon slurry with > 0 to < 10 mols of activator compound per mol of titanium compound in said precursor composition, drying the mixture to obtain a free-flowing solid particulate material, and feeding the precursor composition into the polymerization reactor wherein it is further activated by spraying additional activator compound into the reactor in the form of a solution in a hydrocarbon containing 2 to 30 weight percent of the activator compound, or adding said activator compound absorbed on a carrier material containing 10 to 50 percent by weight of said activator compound, so as to provide ≧ 10 up to a total of ≦ 400 mols of said activator compound per mol of titanium compound in said precursor composition. Ethylene copolymers obtainable by the above-mentioned process, as recovered directly from a polymerization reactor, contain ≧ 90 mol percent of ethylene and ≦ 10 mol percent of at least one C₃ to C₈ α-olefin which does not contain any branching of any carbon atom closer than the fourth carbon atom, are in granular form having an average particle size of 0. 125 to 1.78 mm (0.005 to 0.07 inches) with a Ti content of > 0 to ≦ 10 ppm and a content of one or more of Cl, Br or l of > 0 to ≦ 70 ppm, and have a melt index of ≧ 0.0 to about 100 g/10 min, a high load melt index of about 11 to about 2000 g/10 min, a melt flow ratio of ≧ 22 to ≦ 32, an unsaturated group content of ≦ 1 C = C/1000 carbon atoms, a density of 0.91 to 0.96 g/cm³, a bulk density of 0.24 to 0.50 g/cm³, and a n-hexane extractable content of less than about 3 weight percent. The α-olefins used in the present invention should not contain any branching or any carbon atom closer than the fourth carbon atom. These α-olefins include propylene, butene-1, pentene-1, hexene-1, 4-methyl pentene-1, heptene-1, and octene-1. The preferred α-olefins are propylene, butene-1, hexene-1, 4-methyl pentene-1, and octene-1. The copolymers prepared according to the process of the present invention have a melt flow ratio of ≧ 22 to ≦ 32, and preferably of ≧ 25 to ≦ 30. The melt ratio value is another means of indicating the molecular weight distribution of a polymer. The melt flow ratio (MFR) range of ≧ 22 to ≦ 32 thus corresponds to a Mw/Mn value range of 2.7 to 4.1 and the MFR range of ≧ 25 to ≦ 30 corresponds to a Mw/Mn range of 2.8 to 3.6. The copolymers which may be prepared by the process of the present invention have a density of ≧ 0.91 to ≦ 0.96 g/cm3. The density of the copolymer, at a given melt index level for the copolymer, is primarily regulated by the amount of the C₃ to C₈ comonomer which is copolymerized with the ethylene. In the absence of the comonomer, the ethylene would homopolymerize with the catalyst of the present invention to provide homopolymers having a density of 0.96 g/cm³. Thus, the addition of progressively larger amounts of the comonomers to the reactor results in a progressive lowering of the density of the copolymer. The amount of each of the various C₃ to C₈ comonomers needed to achieve the same result will vary from comonomer to comonomer, under the same reaction conditions. Thus, to achieve the same results in the copolymers, in terms of a given density, at a given melt index level, larger molar amounts of the different comonomers would be needed in the order of C₃ > C₄ > C₅ > C₆ > C₇ > C₈. The melt index of a copolymer is a reflection of its molecular weight. Polymers having a relatively high molecular weight, have a relatively low melt index. Ultrahigh molecular weight ethylene polymers have a high load (HLMI) melt index of about 0.0 g/10 min, and very high molecular weight polymers have a high load melt index (HLMI) of about 0.0 to 1.0 g/10 min. Such high molecular weight polymers are difficult, if not impossible, to mold in conventional injection molding equipment. The polymers made in the process of the present invention, on the other hand, can be readily molded in such equipment. They have a standard or normal load melt index of ≧ 0.0 to 100 g/10 min, and preferably of 0.5 to 80 g/10 min, and a high load melt index (HLMI) of 11 to 2000 g/10 min. The melt index of the copolymers which are made in the process of the present invention is a function of a combination of the polymerization temperature of the reaction, the density of the copolymer and the hydrogen/monomer ratio in the reaction system. Thus, the melt index is raised by increasing the polymerization temperature and/or by decreasing the density of the polymer and/or by increasing the hydrogen/monomer ratio. In addition to hydrogen, other chain transfer agents, such as dialkyl zinc compounds, may also be used to further increase the melt index of the copolymers. The copolymers prepared according to the process of the present invention have an unsaturated group content of ≦ 1, and usually of ≧ 0.1 to ≦ 0.3, C = C/1000 carbon atoms. The copolymers prepared according to the process of the present invention have a n-hexane extractable content (at 50°C) of less than about 3, and preferably, of less than about 2, weight percent. The copolymers prepared according to the process of the present invention have a residual catalyst content, in terms of parts per million of titanium metal, of the order of > 0 to ≦ 20 parts per million (ppm) at a productivity level of ≧ 50,000 kg of polymer per kg of titanium, and of the order of > 0 to ≦ 10 ppm at a productivity level of ≧ 100,000 kg of polymer per kg of titanium and of the order of > 0 to ≦ 3 parts per million at a productivity level of ≧ 300,000 kg of polymer per kg of titanium. In terms of Cl, Br or l residues, the copolymers prepared according to the process of the present invention have a Cl, Br or l residue content which depends upon the Cl, Br or l content of the precursor. From the Ti to Cl, Br or l ratio in the intial precursor, it is possible to calculate Cl, Br or l residues from the knowledge of the productivity level based on titanium residues only. For many of the copolymers made only with Cl containing components of the catalyst system (Cl/Ti = 7), one can calculate a Cl residue content of > 0 to ≦ 140 ppm at a productivity of ≧ 50,000 kg of polymer per kg of titanium, a Cl content of > 0 to ≦ 70 ppm at a productivity of ≧ 100,000 kg of polymer per kg of titanium, and a Cl content of > 0 to ≦ 20 ppm at a productivity of ≧ 300,000 kg of polymer per kg of titanium. The copolymers are readily produced in the process of the present invention at productivities of up to about 1,000,000 kg of polymer per kg of titanium. The copolymers prepared according to the process of the present invention are granular materials which have an average particle size of the order of 0.125 to 0.178 mm (0.005 to 0.07 inches), and preferably, of 0.5 to 1.0 mm (0.02 to 0.04 inches), in diameter. The particle size is important for the purposes of readily fluidizing the polymer particles in the fluid bed reactor, as described below. The copolymers prepared according to the process of the present invention have a bulk density of 0.24 to 0.50 g/cm³ (15 to 31 pounds per cubic foot). For film making purposes the preferred copolymers prepared according to the process of the present invention are those having a density of ≧ 0.912 to ≦ 0.940 g/cm³, and preferably of about ≧ 0.916 to ≦ 0.928 g/cm³, a molecular weight distribution (Mw/Mn) of ≧ 2.7 to ≦ 3.6 and preferably of ≧ 2.8 to ≦ 3.1, and a standard melt index of ≧ 0.5 to ≦ 5.0 g/10 min, and preferably of ≧ 0.7 to ≦ 4.0 g/10 min. For the injection molding of flexible articles such as houseware materials, the preferred copolymers are those having a density of ≧ 0.920 to ≦ 0.940 g/cm³, and preferably, of ≧ 0.925 to ≦ 0.930 g/cm³, a molecular weight distribution Mw/Mn of ≧ 2.7 to ≦ 3.6, and preferably of ≧ 2.8 to ≦ 3.1 and a standard melt index of ≧ 2 to ≦ 100 g/10 min, and preferably, of ≧ 8 to ≦ 80 g/10 min. For the injection molding of rigid articles such as pails, the preferred copolymers are those having a density of ≧ 0.950 to ≦ 0.958 g/cm³, and preferably of ≧ 0.953 to ≧ 0.955 g/cm³, a molecular weight distribution (Mw/Mn) of ≧ 2.7 to ≦ 3.6, and preferably, of ≧ 2.8 to ≦ 3.1, and a standard melt index of ≧ 1 to ≦ 40 g/10 min and preferably of ≧ 5 to ≦ 20 g/10 min. The compounds used to form the high activity catalyst used in the present invention comprise at least one titanium compound, at least one magnesium compound, at least one electron donor compound, at least one activator compount and at least one inert carrier material, as defined below. The titanium compound has the structure Ti(OR) a X b wherein R is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, or COR′ where R′ is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, X is selected from the group consisting of Cl, Br, l, or mixtures thereof a is 0 or 1, b is 2 to 4 inclusive and a + b = 3 or 4. Preferably R and R′ are C₁₋₁₄ alkyl and C₆₋₁₄ aryl, especially C₁₋₈ alkyl, most preferably C₁₋₆ alkyl and C₆₋₁₀ aryl. E.g. methyl, ethyl, propyl, i-propyl, butyl, i-butyl, pentyl, hexyl, octyl, i-octyl, nonyl, decyl, dodecyl; tetradecyl; phenyl, tolyl, xylyl, ethylphenyl, naphthyl. The titanium compounds can be used individually or in combinations thereo, an would include TiCl₃, TiCl₄, Ti(OCH₃)Cl₃, Ti(OC₆H₅)Cl₃, Ti(OCOCH₃)Cl₃ and Ti(OCOC₆H₅)Cl₃. The magnesium compound has the structure MgX₂ wherein X is selected from the group consisting of Cl, Br, l, or mixtures thereof. Such magnesium compounds can be used individually or in combinations thereof and would include MgCl₂, MgBr₂ and Mgl₂. Anhydrous MgCl₂ is the particularly preferred magnesium compound. From 1.5 to 56, and preferably from 1.5 to 10, mols of the magnesium compound are used per mol of the titanium compound in preparing the catalysts employed in the present invention. The titanium compound and the magnesium compound should be used in a form which will facilitate their dissolution in the electron donor compound, as described herein below. The electron donor compound is an organic compound which is liquid at 25°C and in which the titanium compound and the magnesium compound are partially or completely soluble. The electron donor compounds are known as such or as Lewis bases. The electron donor compounds would include such compounds as alkyl esters of aliphatic and aromatic carboxylic acids, aliphatic ethers, cyclic ethers and aliphatic ketones. Among these electron donor compounds the preferable ones are alkyl esters of C₁ to C₄ saturated aliphatic carboxylic acids; alkyl esters of C₇ to C₈ aromatic carboxylic acids; C₂ to C₈, and most preferably C₃ to C₄, aliphatic ethers; C₃ to C₄ cyclicethers, and preferably C₄ cyclic mono- or di-ethers; C₃ to C₆, and most preferably C₃ to C₄, aliphatic ketones. The most preferred of these electron donor compounds would include methyl formate, ethyl acetate, butyl acetate, ethyl ether, hexyl ether, tetrahydrofuran, dioxane, acetone and methyl isobutyl ketone. The electron donor compounds can be used individually or in combinations thereof. From 2 to 85, and preferably from 3 to 10 mols of the electron donor compound are used per mol of Ti. The activator compound has the structure Al(R″) c X′ d H e wherein X′ is Cl or O‴, R″ and R‴ are the same or different and are C₁ to C₁₄ saturated hydrocarbon radicals, d is 0 to 1,5, e is 1 or 0 and c + d + e = 3, Preferably R″ and R‴ are saturated aliphatic C₁₋₁₄ residues (as e.g. mentioned in connection with R and R′) or saturated cycloaliphatic residues with 5-10 carbon atoms such as cyclopentyl, cyclohexyl, cycloheptyl, methylcyclohexyl. Such activator compounds can be used individually or in combinations thereof and would include Al(C₂H₅)₃, Al(C₂H₅)₂Cl, Al(i-C₄H₉)₃, Al₂(C₂H₅)₃Cl₃, Al(i-C₄H₉)₂H, Al(C₆H₁₃)₃, Al(C₈H₁₇)₃, Al(C₂H₅)₂H and Al(C₂H₅)₂(OC₂H₅). From ≧ 10 to ≦ 400, and preferably from 10 to 100, mols of the activator compound are used per mol of the titanium compound in activating the precursor composition employed in the present invention. The carrier materials used in the process of the present invention are solid, particulate materials which are inert to the other components of the catalyst composition, and to the other active components of the reaction system. These carrier materials would include inorganic materials such as oxides of silicon and aluminum and molecular sieves, and organic materials such as olefin polymers such as polyethylene. The carrier materials are used in the form of dry powders having an average particle size of 10 to 250, and preferably of 50 to 150 µm. These materials are also preferably porous and have a surface area of ≧ 3, and preferably of ≧ 50, square meters per gram. The carrier material should be dry, that is, free of absorbed water. Drying of the carrier material is carried out by heating it at a temperature of ≧ 600°C. Alternatively, the carrier material dried at a temperature of ≧ 200°C may be treated with 1 to 8 weight percent of one or more of the aluminum alkyl compounds described above. This modification of the carrier material by the aluminum alkyl compound provides the catalyst composition with increased activity and also improves polymer particle morphology of the resulting ethylene polymers. The catalyst used in the present invention is prepared by first preparing a precursor composition from the titanium compound, the magnesium compound, and the electron donor compound, as described below, and by then treating the precursor composition with the carrier material and the activator compound as described below. The precursor composition is formed by dissolving the titanium compound and the magnesium compound in the electron donor compound at a temperature of 20°C up to the boiling point of the electron donor compound. The titanium compound can be added to the electron donor compound before or after the addition of the magnesium compound, or concurrent therewith. The dissolution of the titanium compound and the magnesium compound can be facilitated by stirring, and, in some instances by refluxing, these two compounds in the electron donor compound. When the titanium compound and the magnesium compound are dissolved, the precursor composition is isolated by crystallization or by precipitation with a C₅ to C₈ aliphatic or aromatic hydrocarbon such as hexane, isopentane or benzene. The crystallized or precipitated precursor composition is isolated in the form of fine, free flowing particles having an average particle size of 10 to 100 µm and a bulk density of 0.289 to 0.529 g/cm³ (18 to 33 pounds per cubic foot). Particle sizes of ≦ 100 µm are preferred for use in a fluid bed process. The particle size of the isolated precursor composition can be controlled by the rate of crystallization or precipitation. When thus made as disclosed above, the precursor composition has the formula Mg m Ti (OR) n X p [ED] q wherein ED is the electron donor compound, m is ≧ 1.5 to ≦ 56, and preferably ≧ 1.5 to ≦ 5.0, n is 0 to 1, p is ≧ 6 to ≦ 116, and preferably ≧ 6 to ≦ 14, q is ≧ 2 to ≦ 85, and preferably ≧ 4 to ≦ 11, R is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, or COR′ wherein R′ is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical and X is selected from the group consisting of Cl, Br, l, or mixture thereof. The polymerization activity of the completely activated catalyst is so high, in the process of the invention, that a dilution of the precursor composition with the carrier material is necessary in order to effectively control the reaction rate. The dilution of the precursor composition can be accomplished before the precursor composition is partially activated, as disclosed below, or concurrent with such activation. The dilution of the precursor composition with the carrier material is accomplished by mechanically mixing or blending 0.33 to 1, and preferably 0.1 to 0.33, parts of the precursor composition with one part by weight of the carrier material. In order to be used in the process of the present invention the precursor composition must be treated with sufficient activator compound to transform the Ti atoms in the precursor composition to an active state. It has been found, however, that the manner of activating the catalyst is very critical in order to obtain an active material, even when an inert carrier is present. Attempts to activate the catalyst by a process similar to that of US-A-3 989 881, for example, wherein the total amount of activator theoretically needed to fully activate the catalyst was added to the precursor composition in a hydrocarbon slurry, followed by drying of the slurry at temperatures of ≧ 20 to ≦ 80°C to remove the solvent therefrom to facilitate the use of the catalyst in a gas phase fluid bed process, produced a product which was not sufficiently active in the process otherwise described below for commercial purposes. It has been found that, in order to prepare a useful catalyst, it is necessary to conduct the activation in such a way that the final activation is conducted in such manner as to avoid the need for drying the fully active catalyst to remove solvent therefrom. According to the present invention the precursor composition is first partially activated outside the polymerization reactor by treating it in a hydrocarbon solvent slurry with > 0 to < 10, preferably 4 to 8, mols of activator compound per mol titanium compound in said precursor composition. The hydrocarbon solvent is then removed by drying and the partially activated precursor composition is fed to the polymerization reactor where activation is completed by treatment with additional activator compound which can be the same or a different compound. In the first stage of the activation the solid particulate precursor composition, diluted with carrier material, is reacted with and partially activated by enough activator compound so as to provide a partially activated precursor composition which has an activator compound/Ti molar ratio of > 0 to < 10: 1, and preferably of 4 to 8: 1. This partial activation reaction is carried out in a hydrocarbon solvent slurry followed by drying of the resulting mixture, to remove the solvent, at temperatures between 20 to 80, and preferably of 50 to 70°C. In this partial activation procedure the activator compound may be used while absorbed on the carrier material used to dilute the activator compound. The resulting product is a free-flowing solid particulate material which can be readily fed to the polymerization reactor. The partially activated precursor composition, however, is, at best, weakly active as a polymerization catalyst in the process of the present invention. In order to render the partially activated precursor composition active for ethylene polymerization purposes, additional activator compound must also be added to the polymerization reactor to complete, in the reactor, the activation of the precursor composition. The additional activator compound and the partially activated precursor composition are preferably fed to the reactor through separate feed lines. The additional activator compound may be sprayed into the reactor in the form of a solution thereof in a hydrocarbon solvent such as isopentane, hexane, or mineral oil. This solution usually contains 2 to 30 weight percent of the activator compound. The activator compound may also be added to the reactor in solid form, by being absorbed on a carrier material. The carrier material usually contains 10 to 50 weight percent of the activator for this purpose. The additional activator compound is added to the reactor in such amounts as to provide, in the reactor with the amounts of activator compound and titanium compound fed with the partially activated precursor composition, from ≧ 10 to ≦ 400 total mols of activator compound per mol of titanium compound in said precursor composition, preferably from 15 to 60 total mols of activator compound per mol of titanium compound in said precursor compound. The additional amounts of activator compound added to the reactor react with, and complete the activation of, the precursor composition in the reactor. In the continuous gas phase fluid bed process disclosed below, discrete portions of the partially activated precursor composition are continuously fed to the reactor, with discrete portions of any additional activator compound needed to complete the activation of the partially activated precursor composition, during the continuing polymerization process in order to replace active catalyst sites that are expended during the course of the reaction. The drawing shows a gas phase liquid bed reactor system for carrying out the process of the present invention. The polymerization reaction is conducted by contacting a stream of the monomers in the fluid bed process described below, and substantially in the absence of catalyst poisons such as moisture, oxygen, CO, CO₂, and acetylene with a catalytically effective amount of the activated precursor composition (the catalyst) at a temperature and at a pressure sufficient to initiate the polymerization reaction. In order to achieve the desired density ranges in the copolymers it is necessary to copolymerize enough of the ≧ C₃ comonomers with ethylene to achieve a level of 0 to 10 mol percent of the C₃ to C₈ comonomer in the copolymer. The amount of comonomer needed to achieve this result will depend on the particular comonomer(s) employed. There is provided below a listing of the amounts, in mols, of various comonomers that must be copolymerized with ethylene in order to provide polymers having the desired density range at any given melt index. The listing also indicates the relative molar concentration, of such comonomer to ethylene, which should be present in the gas stream of monomers which is fed to the reactor. A fluidized bed reaction system which can be used in the practice of the process of the present invention is illustrated in Figure 1. With reference thereto the reactor 10 consists of a reaction zone 12 and a velocity reduction zone 14. The reaction zone 12 comprises a bed of growing polymer particles, formed polymer particles and a minor amount of catalyst particles fluidized by the continuous flow of polymerizable and modifying gaseous components in the form of make-up feed and recycle gas through the reaction zone. To maintain a viable fluidized bed, the mass gas flow rate through the bed must be above the minimum flow required for fluidization, and preferably from 1.5 to 50 times G mf and more preferably from 3 to 6 times G mf . G mf is used in the accepted form as the abbreviation for the minimum mass gas flow required to achieve fluidization, C. Y. Wen and Y. H. Yu, "Mechanics of Fluidization", Chemical Engineering Progress Symposium Series, Vol. 62, p. 100-111 (1966). It is essential that the bed always contains particles to prevent the formation of localized "hot spots" and to entrap and distribute the particulate catalyst throughout the reaction zone. On start up, the reaction zone is usually charged with a base of particulate polymer particles before gas flow is initiated. Such particles may be identical in nature to the polymer to be formed or different therefrom. When different, they are withdrawn with the desired formed polymer particles as the first product. Eventually, a fluidized bed of the desired polymer particles supplants the start-up bed. The partially activated precursor compound used in the fluidized bed is preferably stored for service in a reservoir 32 under a blanket of a gas which is inert to the stored material, such as nitrogen or argon. Fluidization is achieved by a high rate of gas recycle to and through the bed, typically in the order of 50 times the rate of feed or make-up gas. The fluidized bed has the general appearance of a dense mass of viable particles in possible free-vortex flow as created by the percolation of gas through the bed. The pressure drop through the bed is equal to or slightly greater than the mass of the bed divided by the cross-sectional area. It is thus dependent on the geometry of the reactor. Make-up gas is fed to the bed at a rate equal to the rate at which particulate polymer product is withdrawn. The composition of the make-up gas is determined by a gas analyzer 16 positioned above the bed. The gas analyzer determines the composition of the gas being recycled and the composition of the make-up gas is adjusted accordingly to maintain an essentially steady state gaseous composition within the reaction zone. To insure complete fluidization, the recycle gas and, where desired, part of the make-up gas are returned to the reactor at point 18 below the bed. There exists a gas distribution plate 20 above the point of return to aid fluidizing the bed. The portion of the gas stream which does not react in the bed constitutes the recycle gas which is removed from the polymerization zone, preferably by passing it into a velocity reduction zone 14 above the bed where entrained particles are given an opportunity to drop back into the bed. Particle return may be aided by a cyclone 22 which may be part of the velocity reduction zone or exterior thereto. Where desired, the recycle gas may then be passed through a filter 24 designed to remove small particles at high gas flow rates to prevent dust from contacting heat transfer surfaces and compressor blades. The recycle gas is then compressed in a compressor 25 and then passed through a heat exchanger 26 wherein it is stripped of heat of reaction before it is returned to the bed. By constantly removing heat or reaction, no noticeable temperature gradient appears to exist within the upper portion of the bed. A temperature gradient will exist in the bottom of the bed in a layer of 15 to 30 cm (6 to 12 inches), between the temperature of the inlet gas and the temperature of the remainder of the bed. Thus, it has been observed that the bed acts to almost immediately adjust the temperature of the recycle gas above this bottom layer of the bed zone to make it conform to the temperature of the remainder of the bed, thereby maintaining itself at an essentially constant temperature under steady state conditions. The recycle is then returned to the reactor at its base 18 and to the fluidized bed through distribution plate 20. The compressor 25 can also be placed upstream of the heat exchanger 26. The distribution plate 20 plays an important role in the operation of the reactor. The fluidized bed contains growing and formed particulate polymer particles as well as catalyst particles. As the polymer particles are hot and possibly active, they must be prevented from settling, for if a quiescent mass is allowed to exist, any active catalyst contained therein may continue to react and cause fusion. Diffusing recycle gas through the bed at a rate sufficient to maintain fluidization at the base of the bed is, therefore, important. The distribution plate 20 serves this purpose and may be a screen, slotted plate, perforated plate, a plate of the bubble cap type, and the like. The elements of the plate may all be stationary, or the plate may be of the mobile type disclosed in US-A-3 298,792. Whatever its design, it must diffuse the recycle gas through the particles at the base of the bed to keep them in a fluidized condition, and also serve to support a quiescent bed of resin particles when the reactor is not in operation. The mobile elements of the plate may be used to dislodge any polymer particles entrapped in or on the plate. Hydrogen may be used as a chain transfer agent in the polymerization reaction of the present invention. The ratio of hydrogen/ethylene employed will vary between 0 to 2.0 moles of hydrogen per mole of the monomer in the gas stream. Any gas inert to the catalyst and reactants can also be present in the gas stream. The activator compound is preferably added to the reaction system at the hottest portion of the gas, which is usually downstream from heat exchanger 26. Thus, the activator may be fed into the gas recycle system from dispenser 27 thru line 27A. Compounds of the structure Zn(R a )(R b ), wherein R a and R b are the same or different C₁ to C₁₄ aliphatic or aromatic hydrocarbon radicals, may be used in conjunction with hydrogen, with the catalysts of the present invention as molecular weight control or chain transfer agents, that is, to increase the melt index values of the copolymers that are produced. From 0 to 50, and preferably from 20 to 30, mols of the Zn compound would be used in the gas stream in the reactor per mol of titanium compound in the reactor. The zinc compound would be introduced into the reactor, preferably in the form of a dilute solution (2 to 30 weight percent) in hydrocarbon solvent or absorbed on a solid carrier material, such as silica, of the types described above, in amounts of from 10 to 50 weight percent. These compositions tend to be pyrophoric. The zinc compound may be added alone, or with any additional portions of the activator compound that are to be added to the reactor from a feeder, not shown, which could be positioned adjacent dispenser 27, near the hottest portion of the gas recycle system. It is essential to operate the fluid bed reactor at a temperature below the sintering temperature of the polymer particles. To insure that sintering will not occur, operating temperatures below the sintering temperature are desired. For the production of ethylene copolymers in the process of the present invention an operating temperature of from 30 to 115°C is preferred, and a temperature of from 75 to 95°C is most preferred. Temperatures of from 75 to 90°C are used to prepare products having a density of from 0.91 to 0.92 g/cm³, and temperatures of from 80 to 100°C are used to prepare products having a density of from > 0.92 to 0.94 g/cm³, and temperatures of from 90 to 115°C are used to prepare products having a density of from > 0.94 to 0.96 g/cm³. The fluid bed reactor is operated at pressures of up to 69 bar (1000 psi), and is preferably operated at a pressure of from 10.3 to 24 bar (150 to 350 psi), with operation at the higher pressures in such ranges favoring heat transfer since an increase in pressure increases the unit volume heat capacity of the gas. The partially activated precursor composition is injected into the bed at a rate equal to its consumption at a point 30 which is above the distribution plate 20. Injecting the precursor composition at a point above the distribution plate is an important feature of this invention. Since the catalysts used in the practice of the invention are highly active, injection of the precursor composition into the area below the distribution plate may cause polymerization to begin there and eventually cause plugging of the distribution plate. Injection into the viable bed, instead, aids in distributing the catalyst throughout the bed and tends to preclude the formation of localized spots of high catalyst concentration which may result in the formation of "hot spots". A gas which is inert to the catalyst, such as nitrogen or argon, is used to carry the partially activated precursor composition, and any additional activator compound or non-gaseous chain transfer agent that is needed, into the bed. The production rate is controlled by the rate of catalyst injection. The production rate may be increased by simply increasing the rate of catalyst injection and decreased by reducing the rate of catalyst injection. Since any change in the rate of catalyst injection will change the rate of generation of the heat of reaction, the temperature of the recycle gas is adjusted upwards or downwards to accommodate the change in rate of heat generation. This insures the maintenance of an essentially constant temperature in the bed. Complete instrumentation of both the fluidized bed and the recycle gas cooling system, is, of course, necessary to detect any temperature change in the bed so as to enable the operator to make a suitable adjustment in the temperature of the recycle gas. Under a given set of operating conditions, the fluidized bed is maintained at essentially a constant height by withdrawing a portion of the bed as product at a rate equal to the rate of formation of the particulate polymer product. Since the rate of heat generation is directly related to product formation, a measurement of the temperature rise of the gas across the reactor the difference between inlet gas temperature and exit gas temperature) is determinative of the rate of particulate polymer formation at a constant gas velocity. The particulate polymer product is preferably continuously withdrawn at a point 34 at or close to the distribution plate 20, and in suspension with a portion of the gas stream which is vented before the particles settle to preclude further polymerization and sintering when the particles reach their ultimate collection zone. The suspending gas may also be used, as mentioned above, to drive the product of one reactor to another reactor. The particulate polymer product is conventiently and preferably withdrawn through the sequential operation of a pair of timed valves 36 and 38 defining a segregation zone 40. While valve 38 is closed, valve 36 is opened to emit a plug of gas and product to the zone 40 between it and valve 36 which is then closed. Valve 38 is then opened to deliver the product to an external recovery zone. Valve 38 is then closed to await the next product recovery operation. ' Finally, the fluidized bed reactor is equipped with an adequate venting system to allow venting the bed during start up and shut down. The reactor does not require the use of stirring means and/or wall scraping means. The highly active catalyst system of this invention appears to yield a fluid bed product having an average particle size between 0.125 to 1.78 mm (0.005 to 0.07 inches) and preferably 0.5 to 1.0 mm (0.02 to 0.04 inches). The feed stream of gaseous monomer, with or without inert gaseous diluents, is fed into the reactor so as to maintain a space time yield of 32 to 160 kg/h/m³ (2 to 10 pounds/hours/cubic foot) of bed volume. The polymer directly recovered from the polymerization reactor is in granular form ("virgin" polymer). 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 For materials having a density < 0.940 g/cm³, ASTM-1505 procedure is used and plaque is conditioned for one hour at 100°C to approach equilibrium crystallinity. For materials having a density of ≧ 0.940 g/cm³, a modified procedure is used wherein the test plaque is conditioned for one hour at 120°C to approach equilibrium crystallinity and is then quickly cooled to room temperature. All density values are reported as g/cm³. All density measurements are made in a density gradient column. Melt index (MI) ASTM D-1238-Condition E-Measured at 190°C-reported as g/10 min. FLow rate (HLMI) ASTM D-1238-Condition F-Measured at 10 times the weight used in the melt index test above. Melt flow ration (MFR)= Flow rate Melt index Productivity A sample of the resin product is ashed, and the weight % of ash is determined; since the ash is essentially composed of the catalyst, the productivity is thus the kg of polymer produced per kg of total catalyst consumed. The amount of Ti, Mg and Cl in the ash are determined by elemental analysis. Film rating A sample of film is viewed with the naked eye to note the size and distribution of gels or other foreign particles in comparison to standard film samples. The appearance of the film, as thus compared to the standard samples, is then given a rating on a scale of - 100 (very poor) to + 100 (excellent). n-hexane extractables (FDA test used for polyethylene film intended for food contact applications). A 1.29 m (200 square inch) sample of 0.030 mm (1.5 mil) gauge film is cut into strips measuring 2.5 × 15 cm (1″ × 6″) and weighed to the nearest 0.1 mg. The strips are placed in a vessel and extracted with 300 ml of n-hexane at 50 ± 1°C for 2 hours. The extract is then decanted into tared culture dishes. After drying the extract in a vacuum desiccator, the culture dish is weighed to the nearest 0.1 mg. The extract, normalized with respect to the original sample weight, is then reported as the weight fraction of n-hexane extractables. Bulk density The resin is poured via 9.5 mm (3/8″) diameter funnel into a 100 ml graduated cylinder to 100 ml line without shaking the cylinder, and weighed by difference. Molecular weight distribution (Mw/Mn) Gel Permeation Chromatography. For resins with density 0.94 g/cm³, Styrogel Packing: (Pore Size Sequence is 10⁶, 10⁴, 10³, 10², 6 nm) Solvent is Perchloroethylene at 117°C. For resins with density ≧ 0.94 g/cm³: Styrogel Packing: (Pore Size Sequence is 10⁶, 10⁵, 10⁴, 10³ 6 nm) Solvent is o-dichloro benzene at 135°C. Detection for all resins: Infra red at 3.45 µm. Examples I. Preparation of precursor composition In a 5 liter flask equipped with a mechanical stirrer, 16.0 g (0.168 Mol) of anhydrous MgCl₂ was mixed with 850 ml of pure tetrahydrofuran under nitrogen. The mixture was stirred at room temperature (∼ 25°C) while 13.05 g (0.069 Mol) of TiCl₄ was added dropwise. After complete addition, the contents of the flask were heated to reflux for about 1/2 to 1 hour to dissolve the solids. The system was cooled to room temperature and 3 liters of pure n-hexane was slowly added over a period of 1/4 hour. A yellow solid precipitated. The supernatant was decanted and the solids were washed 3 times with one liter of n-hexane. The solids were filtered and dried in a rotating evaporating flask at 40-60°C to give 55 g of solid precursor composition. The precursor composition may be analyzed at this point for Mg and Ti content since some of the Mg and/or Ti compound may have been lost during the isolation of the precursor composition. The empirical formulas used herein in reporting these precursor compositions are derived by assuming that the Mg and the Ti still exist in the form of the compounds in which they were first added to the electron donor compound and that all other residual weight in the precursor composition is due to the electron donor compound. Analysis of the solid showed the following: Mg: 6.1%; Ti: 4.9%: which corresponds to TiMg 2.45 Cl 8.9 (THF) 7.0 THF means tetrahydrofuran. II. Activation procedures The activation is conducted in such a way that the precursor composition is only partially activated prior to the introduction thereof into the polymerization reactor, and then the remainder of the activation process is completed within such reactor. The desired weight of dry inert carrier material is charged to a mixing vessel or tank. For the examples described herein, the amount of inert carrier is 500 grams for silica and 1000 grams for a polyethylene carrier. The inert carrier material is then admixed with sufficient amounts of anhydrous, aliphatic hydrocarbon diluent, such as isopentane, to provide a slurry system. This usually requires 4 to 7 ml of diluent per gram of inert carrier. The desired weight of the precursor composition is then charged to the mixing vessel and thoroughly admixed with the slurry composition. The amount of precursor composition used in this procedure for making the catalysts in these examples is 80 to 135 grams, with such precursor composition having an elemental titanium content of 1 ± 0.1 millimole of Ti per gram of precursor composition. The desired amount of activator compound needed to partially activate the precursor composition is added to the contents of the mixing vessel so as to partially activate the precursor composition. The amount of activator compound used in this regard provides an Al/Ti ratio in the partially activated precursor composition of > to < 10: 1, and preferably of 4 to 8: 1. The activator compound is added to the mixing tank in the form of a solution which contains 20 weight percent of the activator compound (triethyl aluminum in these examples) in an inert aliphatic hydrocarbon, solvent (hexane in these examples). The activation is accomplished by thoroughly mixing and contacting the activator compound with the precursor composition. All of the operations described above are conducted at room temperature, and at atmospheric pressure in an inert atmosphere. The resulting slurry is then dried under a purge of dry inert gas, such as nitrogen or argon, at atmospheric pressure at a temperature of ≦ 60°C to remove the hydrocarbon diluent. This process usually requires 3 to 5 hours. The resulting product is in the form of a dry free-flowing particulate material wherein the partially activated precursor composition is uniformly blended with the inert carrier. The dried product is stored under an inert gas. In order to complete the activation of the partially activated precursor composition, additional activator compound is fed to the polymerization reactor absorbed on an inert carrier material, such as silica or polyethylene, or, most preferably, a dilute solution in a hydrocarbon solvent such as isopentane. When the activator compound is to be absorbed on a silica carrier the two materials are mixed in a vessel containing about 4 ml of isopentane per gram of carrier material. The resulting slurry is then dried for about 3 to 5 hours under a purge of nitrogen at atmospheric pressure at a temperature of 65 ± 10°C to remove the hydrocarbon diluent. When the activator compound is to be injected into the polymerization reaction system as a dilute solution, concentrations of about 5 to 10% by weight are preferred. Regardless of the method used to introduce the activator compound into the polymerization reactor for the purpose of completing the activation of the precursor composition, it is added at a rate such as to maintain the Al/Ti ratio in the polymerization reactor at a level of ≧ 10 to 400: 1, and preferably of ≧ 10 to 100: 1. Prior to being used herein, the silicas are dried at ≧ 200°C for ≧ 4 hours. Examples 1 to 15 Ethylene was copolymerized with propylene or butene-1 (propylene in Examples 1 to 7 and butene-1 in Examples 8 to 15) in each of this series of 15 examples with catalysts formed and activated as described above to produce polymers having a density of > 0.940 g/cm³. In each case the partially activated precursor composition had an Al/Ti mol ratio of 2.4 to 5.0. The completion of the activation of the precursor composition in the polymerization reactor was accomplished with triethyl aluminum as either a 2.6 or 5 weight% solution in isopentane so as to provide the completely activated catalyst in the reactor with an Al/Ti mol ratio of about 12 to 47. Each of the polymerization reactions was continuously conducted for > 1 hour after equilibrium was reached and under a pressure of 22 bar (300 psig) and a gas velocity of 5 to 6 times G mf in a fluid bed reactor system at a space time yield of 48 to 96 kg/g/m³ (3 to 6 lbs/hr/ft³) of bed space. The reaction system was as described above. It has a lower section 3 m (10 feet) high and 34 cm (13 1/2 inches) in (inner) diameter, and an upper section which was 4.8 m (16 feet) high and 59 cm (23 1/2 inches) in (inner) diameter. In several of the examples zinc diethyl was added during the reaction (as a 2.6 weight% solution in isopentane) to maintain a constant Zn/Ti mol ratio. Where the zinc diethyl was used, the triethyl aluminum was also added as a 2.6 weight% solution in isopentane. Table I below lists, with respect to Examples 1 to 15, various operating conditions employed in such examples i.e., the weight% of precursor composition in the blend of silica and precursor composition; Al/Ti ratio in the partially activated precursor composition; Al/Ti ratio maintained in the reactor; polymerization temperature; % by volume of ethylene in reactor; H₂/ethylene mol ratio in reactor; comonomer (C x )/C₂ mol ratio in reactor; catalyst productivity and Zn/Ti mol ratio. Table II below lists properties of the granular copolymers as directly obtained from the reactor ("virgin resins") made in Examples 1 to 15, i.e. density; melt index (M.I.); melt flow ratio (MFR); weight% ash; Ti content (ppm); bulk density and average particle size. Examples 16 to 28 Ethylene was copolymerized with propylene or butene-1 (propylene in Examples 16 to 17 and butene-1 in Examples 18 to 28) in each of this series of 14 examples with catalysts formed and activated as described above to produce polymers having a density of ≦ 0.940 g/cm³. In each case, the partially activated precursor composition had an Al/Ti mol ratio of 4.4 to 5.8. The completion of the activation of the precursor composition in the polymerization reactor was accomplished with triethyl aluminum (as a 5 weight% solution in isopentane in Examples 16 to 18 and 21 to 28, and adsorbed on silica, 50/50 weight%, in Examples 19 and 20) so as to provide the completely activated catalyst in the reactor with an Al/Ti mol ratio of about 27 to 140. Each of the reactions were conducted as in Examples 1 to 15. Table III listsoperating conditions used in Examples 16 to 28 and Table IV lists properties of the granular virgin resins made in such examples. Unsaturation is measured with an infrared spectrophotometer (Perkin Elmer Model 21). Pressings made from the resin which are 0.63 mm (25 mils) in thickness are used as test specimens. Absorbance is measured at 10.35 µm for transvinylene unsaturation, 11.0 µm for terminal vinyl unsaturation and 11.25 µm for pendant vinylidene unsaturation. The absorbance per mil of thickness of the pressing is directly proportional to the product of unsaturation concentration and absorptivity. Absorptivities are taken from the literature values of R. J. deKock, et al, J. Polymer Science, Part B. 2, 339 (1964).

Claims: 1. A process for copolymerizing ethylene employing a catalyst composition prepared by forming a precursor composition from a magnesium compound, titanium compound and electron donor compound, and then activating the precursor composition with an organoaluminum compound to form the catalyst, characterized in that the polymerization is conducted continuously in a fluid bed reactor at a temperature of from 30 to 115°C under a pressure of < 69 bar (< 1000 psi) in the gas phase by contacting a mixture of ethylene and one or more C₃ to C₈ α-olefin monomers, said mixture containing from 0 to 2.0 moles of hydrogen per mol of ethylene, with particles of an activated precursor composition wherein said precursor composition has the formula Mg m Ti(OR) n X p [ED] q wherein m is ≧ 1.5 to ≦ 56 n is 0 or 1 p is ≧ 6 to ≦ 116 q is ≧ 2 to ≦ 85 R is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, or COR′ wherein R′ is a C₁ to C₁₄ aliphatic or aromatic hydrocarbon radical, X is selected from the group consisting of Cl, Br, l or mixtures thereof: ED is a liquid organic electron donor compound in which said precursor composition and the Ti and Mg components thereof are partially or completely soluble and which is selected from the group consisting of alkyl esters of aliphatic and aromatic carboxylic acids, aliphatic ethers, cyclic ethers and aliphatic ketones, said precursor composition having an average particle size of 10 to 100 mm, a bulk density of 0.289 to 0.529 g/cm³ (18 to 33 pounds per cubic foot), and being mechanically mixed or blended with at least one solid inert carrier material in a ratio of 0.033 to 1 part of precursor composition per part by weight of carrier material, said carrier material being optionally pretreated with about 1 to 8 weight percent of one or more aluminum alkyl compounds, and being activated with an activator compound having the formula Al(R″) c X′ d H e wherein X′ is Cl or OR‴, R″ and R‴ are the same or different and are C₁ to C₁₄ saturated hydrocarbon radicals d is 0 to 1.5, e is 0 or 1, and c + d + e = 3 activation of said precursor composition being effected by treating said precursor composition outside the polymerization reactor in a hydrocarbon slurry with > 0 to < 10 mols of activator compound per mol of titanium compound in said precursor composition, drying the mixture to obtain a free-flowing solid particulate material, and feeding the precursor composition into the polymerization reactor wherein it is further activated by spraying additional activator compound into the reactor in the form of a solution in a hydrocarbon containing 2 to 30 weight percent of the activator compound, or adding said activator compound absorbed on a carrier material containing 10 to 50 percent by weight of said activator compound, so as to provide ≧ 10 up to a total of ≦ 400 mols of said activator compound per mol of titanium compound in said precursor composition. 2. A process as in claim 1 in which said precursor composition is prepared by dissolving at least one magnesium compound and at least one titanium compound in said electron donor compound and by then recovering said precursor composition by precipitating or crystallizing it from said solution, said magnesium compound having the structure MgX₂ said titanium compound having the structure Ti(OR) a X b wherein a is 0 or 1, b is 2 to 4 and a + b = 3 or 4, and said magnesium compound, said titanium compound and said electron donor compound being employed in such amounts as to satisfy the values of m, n, p and q.

Inventors: FRAZER, WILLIAM ALLEN, FRIIS, NILS, GOEKE, GEORGE LEONARD, JORGENSEN, ROBERT JAMES, KAROL, FREDERICK JOHN, WAGNER, BURKHARD ERIC
Applicants: UNION CARBIDE CORPORATION
Application year: 1979
Main classification: C08F210
IPC codes: C08F2, C08F210