POLYMERIZATION OF COPOLYMERS OF ETHYLENE/PROPYLENE WITH HIGHER OLEFINS

Abstract: A polymer obtained from a first olefin having fewer than 4 carbon atoms, and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms. The molar proportion of the first olefin to the second olefin in the polymer is from 90:10 to 99,9:0,1. A process for producing the polymer is also provided.

Description: POLYMERIZATION OF COPOLYMERS OF ETHYLENE/PROPYLENE WITH HIGHER OLEFINS THIS INVENTION relates to polymerization. More particularly, it relates to copolymers, and to a process for producing such copolymers . According to a first aspect of the invention, there is provided a polymer obtained from a first olefin having fewer than 4 carbon atoms, and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99,9:0,1. According to a second aspect of the invention, there is provided a polymer which comprises a polymerization product obtained by polymerizing at least a first olefin having fewer than 4 carbon atoms and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99, 9:0,1. The polymer may, in particular, be a copolymer of the first olefin with the second olefin. According to a third aspect of the invention, there if provided a copolymer of a first olefin having fewer than 4 carbon atoms, and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99,9:0,1. The second olefin may be 1-heptene, 1-nonene, or 1- undecene, with 1-heptene and 1-nonene being preferred. The olefins can be those obtained from a Fischer-Tropsch process; however, instead the olefins can be those obtained from another process provided that they are poly erizable, ie provided they can be polymerized with known catalysts. The copolymers according to this invention are thermoplastic, and can readily be processed into articles by injection moulding, blow moulding, compression moulding, extrusion and thermoforming. These copolymers have a high impact strength which increases with increasing content of the second olefin. On the other hand, tensile properties decrease moderately with an increase in the content of the second olefin in the copolymer; however, the tensile properties remain in the area of suitable application of articles obtained by the techniques mentioned hereinbefore. The copolymers according to the invention may have: a) a melt flow index, as measured according to ASTM D 1238, in the range of 0,01 to 50dg/min; and b) an Izod notched impact strength, as measured according to ASTM D 256, greater than 5 kJ/m 2 ; and/or c) a tensile strength at yield, as measured according to ASTM D 638 M, greater than 5 MPa; and/or d) a modulus, as measured according to ASTM D 638 M, greater than 100 MPa. The Applicant has ascertained that within the family of copolymers of the first olefin with the second olefin according to this invention, there are particular subfamilies with surprising application properties. Thus, the sub- family of copolymers of ethylene with the second olefin have different application properties to the sub-family of copolymers of propylene with the second olefin. In a first embodiment of the invention, the first olefin may be ethylene . The copolymers according to the first embodiment of the invention may have: a) a melt flow index, as measured according to ASTM D 1238, in the range of 0,01 to 50dg/min; and b) a density as measured according to ASTM D 1505, in the range of 0,910 and 0,950gm/cm 3 ; and/or c) an Izod notched impact strength, as measured according to ASTM D 256, greater than 5 kJ/m 2 ; and/or d) a tensile strength at yield, as measured according to ASTM D 638 M, greater than 5 MPa; and/or e) a modulus, as measured according to ASTM D 638 M, greater than 100 MPa. The Applicant has surprisingly found that within the subfamily of copolymers of ethylene with the second olefin as obtained according to this invention, there are particular groups with even more surprising application properties. Thus, copolymers of ethylene with 1-heptene as the second olefin have surprisingly been found to have different application properties to copolymers of ethylene with 1-nonene as the second olefin. These properties cannot be correlated to a mathematical relationship between the carbon numbers of the respective second olefins . Thus, in one version of the first embodiment of the invention, there is provided a copolymer of ethylene with 1-heptene . A preferred content of 1-heptene in the copolymer of ethylene with 1-heptene according to this invention, is between 0 , 2 mol percent and 2 mol percent . The copolymer of ethylene and 1-heptene according to this invention may have: a) a melt flow, index as measured according to ASTM D1238, in the range of 0,01 to 50dg/min; and/or b) a density as measured according to ASTM D 1505, in the range of 0,910 and 0,950gm/cm 3 ; and/or c) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 10 [C 7 ] where [C 7 ] is the molar concentration of 1-heptene in the polymer; and/or d) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -4.4 [C 7 ] + 17 ; and/or e) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -275 [C 7 ] + 850 ; and/or f) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -10 [C 7 ] + 56 In another version of the first embodiment of the invention, there is provided a copolymer of ethylene with 1-nonene . A preferred content of 1-nonene in the copolymer of ethylene with 1-nonene according to this invention, is between 0,1 mol percent and 1,5 mol percent. The copolymer of ethylene and 1-nonene according to this invention may have: a) a melt flow index, as measured according to ASTM D 1238, in the range of 0,01 to 50dg/min ; and/or b) a density as measured according to ASTM D 1505, in the range of 0,910 and 0,950gm/cm 3 ; and/or c) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 13.3[C 9 ] where [C 9 ] is the molar concentration of 1-nonene; and/or d) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -16.67 [C 9 ] + 25 ; and/or e) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -666.67 [C 9 ] + 1100 ; and/or f) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -30 [C 9 ] + 65 In a second embodiment of the invention, the first olefin may be propylene . The Applicant has surprisingly found that within the subfamily of copolymers of propylene with the second olefin as obtained according to this invention, there are particular groups with even more surprising application properties. Thus, copolymers of propylene with 1-heptene as the second olefin have surprisingly been found to have different application properties to copolymers of propylene with 1-nonene as the second olefin. The changes in the values of the application properties cannot be correlated to a mathematical relationship between the carbon numbers of the respective second olefins. Thus, in one version of the second embodiment of the invention, there is provided a copolymer of propylene with 1-heptene . A preferred content of 1-heptene in the copolymer of propylene and 1-heptene according to this invention, is between 0,2 mol percent and 2 mol percent. The copolymer of propylene and 1-heptene according to this invention may have-. a) a melt flow index as measured according to ASTM D 1238, in the range of 0,01 to 50dg/min; and/or b) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 7.5 [C 7 ] where [C 7 ] is the molar concentration of 1-heptene in the polymer; and/or c) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -7[C 7 ] + 24 ; and/or d) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation-. E > -350 [C 7 ] + 1000 ; and/or e) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -7.2 [C 7 ] + 63 In another version of the second embodiment ■ of the invention, there is provided a copolymer of propylene with 1-nonene . A preferred content of 1-nonene in the copolymer of propylene and 1-nonene according to this invention, is between 0,1 mol percent and 1,5 mol percent. The copolymer of propylene and 1-nonene according to this invention may have: a) a melt flow index as measured according to ASTM D1238, in the range of 0,01 to 50dg/min; and/or b) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 15 [C 9 ] where [C 9 ] is the molar concentration of 1-nonene in the polymer; and/or c) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -5.3 [C 9 ] + 24 ; and/or d) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -333.3 tC 9 ] + 1000 ; and/or e) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -6.67[C 9 ] + 65 In particular, the copolymers may be obtained by reacting the first olefin with the second olefin in one or more reaction zones, while maintaining in the reaction zone(s) a pressure in the range between atmospheric and 200 kg/cm 2 and a temperature between ambient and 300°C, in the presence of a suitable catalyst or catalyst system. The Applicant has also found that in the copolymerization of the first olefin with the second olefin, specific and different copolymers are obtained when different specific process conditions are employed. Thus, according to a fourth aspect of the invention, there is provided a process for producing a polymer, which process comprises reacting a reaction mixture comprising, as a first monomer, a first olefin having fewer than 4 carbon atoms and, as a second monomer, a second olefin having a total number of carbon atoms greater than 5 and • having an uneven number of carbon atoms , in one or more reaction zones, while maintaining the reaction zone(s) at a pressure between atmospheric pressure and 200kg/cm 2 , and at a temperature between ambient and 300°C, in the presence of a catalyst system or a catalyst system comprising a catalyst and a cocatalyst, such that the molar proportion of the first olefin to the second olefin in the resultant polymer is from 90:10 to 99,9:0,1. The reaction zone(s) may be provided in a single stage reactor vessel or by a chain of two or more reaction vessels . Copolymers obtained from the process by using a particular feed composition and under particular reaction conditions have a random distribution which is determined mainly by the different reactivities of the monomers. This provides a unique tool for obtaining a large variety of copolymers of the first olefin with the second olefin, whose properties are mainly controlled by their composition and non-uniformity . The molecular weight of the resultant random copolymer can be regulated by hydrogen addition to the reaction zone(s) during the reaction. The greater the amount of hydrogen added, the lower the molecular weight of the random copolymer . The copolymerization is preferably performed in a substantially oxygen and water free state, and may be effected in the presence or absence of an inert saturated hydrocarbon The copolymerization reaction may be carried out in a slurry phase, a solution phase or a vapour phase, with slurry phase polymerization being preferred. When slurry phase polymerization is used, the catalyst will be in solid form, and preferably comprises a Ziegler-Natta catalyst. A catalyst system comprising a titanium based Ziegler-Natta catalyst and, as cocatalyst, an organo aluminium compound, is preferred. Thus, the comonomers will be polymerized in a suspension state in the presence of the Ziegler-Natta catalyst which is in solid form and suspended in a slurrying or suspension agent. When vapour phase polymerization is used, the catalyst may also be in solid form, and preferably comprises a Ziegler-Natta catalyst. More particularly a silica supported catalyst or a prepolymerized catalyst or a polymer diluted catalyst may then be used. A catalyst system comprising a titanium based Ziegler-Natta catalyst and, as cocatalyst, an organo aluminium compound, is preferred. Most preferred is a prepolymerized titanium catalyst and a polymer diluted titanium catalyst. In a first embodiment of this aspect of the invention, ethylene may be copolymerized with 1-heptene or 1-nonene. The Applicant has found that in the copolymerization of ethylene with 1-heptene or 1-nonene, particular and different copolymers are obtained when different specific process conditions are employed. Any Ziegler-Natta catalyst suitable for ethylene copolymerization may, at least in principle, be used. Catalysts normally used for the copolymerization of ethylene with other olefins are preferred. However, the most preferred catalysts for the copolymerization of ethylene and 1-heptene or 1-nonene are magnesium chloride supported titanium catalysts, as hereinafter described. Thus, in the preferred catalysts, magnesium chloride is the catalyst support. The magnesium chloride may be used in the form of anhydrous magnesium chloride, or may have a water content between 0.02 mole of water/1 mole of magnesium chloride and 2 mole of water per 1 mole of magnesium chloride, ie it may be partially anhydrized. Most preferably, when the magnesium chloride is partially anhydrized, the water content of the magnesium chloride being, in one particular case, 1,5%, and, in a second particular case, 5% by mass. The anhydrous or partially anhydrized magnesium chloride is preferably activated prior to contacting or loading it with the titanium tetrachloride . The activation of the magnesium chloride may be performed under inert conditions, i.e. in a substantially oxygen and water free atmosphere, and in the absence or in the presence of an inert saturated hydrocarbon liquid. Preferred inert saturated hydrocarbon liquids are aliphatic or cyclo-aliphatic liquid hydrocarbons, of which the most preferred are hexane and heptane. The magnesium chloride or support activation may be performed in two steps designated (a 1 ) and (a 2 ) respectively. In step ( a λ ) , a complexing agent is added under inert conditions to a suspension of the magnesium chloride in the inert hydrocarbon liquid or to the magnesium chloride in powder form. The complexing agent may be selected from the class of an alcohol or a mixture of an alcohol and an ether. Each different alcohol, alcohol mixture, or alcohol mixture with an ether or with different ethers, will give a particular catalyst having different performances. The alcohol may be a linear or branched alcohol with a total number of carbon atoms between 2 and 16. It is preferred to use a mixture of alcohols, with the most preferred being mixtures of linear and branched alcohols. When a linear alcohol is used, between 0,02 mole of alcohol/1 mole of magnesium chloride and 2 mole of alcohol/per 1 mole of magnesium chloride, may be used. When a branched alcohol or a mixture of linear and branched alcohols is used, between 0,015 mole of alcohol/mole of magnesium chloride and 1,5 mole of alcohol/mole of magnesium chloride, may be used. The ether may be an ether with a total carbon number, ie a total number of carbon atoms, of 8 to 16. Either a single ether or a mixture of ethers can be used. When mixtures of linear alcohols and ethers are used, between 0,01 mole of alcohol/ether mixture per 1 mole of magnesium chloride and 2 mole of alcohol/ether mixture per 1 mole of magnesium chloride, may be used. Most preferred are mixtures of branched alcohols and ethers, in which case between 0,05 mole of alcohol/ether mixture per 1 mole of magnesium chloride and 1.5 mole of alcohol/ether mixture per 1 mole of magnesium chloride, may be used. The Applicant has surprisingly found that by using different complexing agents, catalysts with different performances are obtained. Thus, when a mixture of a branched alcohol and an ether is used, the productivity of the catalyst is higher than when a mixture of a linear alcohol and an ether is used. When an alcohol alone is used alone, the productivity was found to be lower than when a mixture of an alcohol with an ether is used. Branched alcohols, when used alone, gave higher productivities than linear alcohols. The resultant mixture or suspension may be stirred for a period of 10 minutes to 24 hours at room temperature. The preferred stirring time is 1 to 12 hours. The preferred temperature for preparing the partially activated magnesium chloride is 40°C to 140 °C. A partially activated magnesium chloride is thus obtained. In the second step (a 2 ) , an alkyl aluminium compound is added, preferably in dropwise fashion, to the partially activated magnesium chloride. Typical alkyl aluminium compounds which can be used are those expressed by the formula AlR 3 wherein R is an alkyl radical or radical component of 1 to 10 carbon atoms. Specific examples of suitable alkyl aluminium compounds, which can be used, are: tri-butyl aluminium, tri-isobutyl aluminium, tri-hexyl aluminium and tri-octyl aluminium. The preferred organo-aluminium compound is tri-ethyl aluminium. The molar ratio of the alkyl aluminium compound to the anhydrous or partially anhydrized magnesium chloride initially used may be between 1:1 and 6:1. The preferred molar ratio of the alkyl aluminium compound to the magnesium chloride is 4:1 to 5:1. The loading of the activated magnesium chloride or support with the titanium tetrachloride may be performed in two steps, designated (b χ ) and (b 2 ) respectively. In the first step (b χ ) , to the support, after thorough washing thereof with hexane, is added an alcohol under stirring. The activated support may be in the form of a suspension in an inert saturated hydrocarbon liquid, as hereinbefore described. The alcohol may be selected from the range of alcohols having 2 to 8 carbon atoms . A dicomponent alcohol mixture can be used. The most preferred method is to use a dicomponent alcohol mixture comprising two alcohols having, respectively, the same number of carbon atoms as the two monomers used in the process of polymerization wherein the catalyst, the product of this catalyst preparation, is used. The molar ratio of the alcohol mixture to the initial magnesium chloride used may be between 0,4:1 and 4:1. However, the preferred molar ratio of the alcohol mixture to the initial magnesium chloride is 0,8:1 to 2,5:1. The molar ratio between the two alcohols in a dicomponent mixture can be from 100:1 to 1:100. However, the preferred molar ratio between the two alcohols is 1:1. The stirring time may be between 1 min and 10 hours, preferably about 3 hours . The temperature during the stirring can be between 0°C and the lowest boiling point of any one of the alcohols in the multicomponent mixture or the inert saturated hydrocarbon liquid when used in this step of the catalyst preparation. In the second step (b 2 ) , titanium chloride, TiCl 4 , is added to the support/alcohol mixture, the resultant mixture or slurry stirred under reflux, and finally left to cool, e.g. for about 24 hours. The catalyst obtained may be thoroughly washed, e.g. with hexane. The molar ratio of TiCl 4 employed in this step to the initial magnesium chloride may be from about 2:1 to about 20:1, preferably about 10:1. When a cocatalyst is employed in the polymerization, it may, as stated hereinbefore, be an organo aluminium compound. Typical organo-aluminium compounds which can be used are compounds expressed by the formula AlR m X 3 _ m wherein R is a hydrocarbon component of 1 to 15 carbon atoms, X is a halogen atom, and m is an integer represented by 0 < m ≤ 3. Specific examples of suitable organo aluminium compounds that can be used are: a trialkyl aluminium, a trialkenyl aluminium, a partially halogenated alkyl aluminium, an alkyl aluminium sesquihalide, an alkyl aluminium dihalide. Preferred organo aluminium compounds are alkyl aluminium compounds, and the most preferred compound is triethylaluminium. The atomic ratio of aluminium to titanium in the catalyst system may be between 0,1:1 and 500:1, preferably between 1:1 and 100:1. For slurry phase copolymerization, preferred slurrying or suspension agents are aliphatic or cyclo-aliphatic liquid hydrocarbons, with the most preferred being hexane and heptane. While the reaction temperature can be in the range of ambient to 300°C, it is preferably in the range of 50°C to 100°C, and most preferably in the range of 60°C to 90°C. While the pressure can be in the range of atmospheric pressure to 200kg/cm 2 , it is preferably in the range of 3kg/cm 2 to 30kg/cm 2 , still more preferably in the range of 4kg/cm 2 to 18kg/cm 2 . When using a catalyst prepared in accordance with the catalyst preparation process hereinbefore described, the parameters of the copolymerization reaction of ethylene with 1-heptene or 1-nonene are thus such that the resultant copolymer of ethylene with 1-heptene or 1-nonene is as hereinbefore described. In another embodiment of this aspect of the invention, propylene may be copolymerized with 1-heptene or 1-nonene. The Applicant has found that in the copolymerization of propylene with 1-heptene or 1-nonene, particular and different copolymers are obtained when different specific process conditions are employed. Any Ziegler-Natta catalyst suitable for propylene copolymerization, at least in principle, may be used. Catalysts used for the copolymerization of propylene with other olefins are preferred. Typical titanium components of Ziegler-Natta catalysts suitable for propylene copolymerization are titanium trichloride and titanium tetrachloride, which may be carried on a support . Catalyst support and activation can be effected in known fashion. For the preparation of the titanium catalyst, halides or alcoholates of trivalent or tetravalent titanium can be used. In addition to the trivalent and tetravalent titanium compounds, and the support or carrier, the catalyst can also contain electron donor compounds, e.g. mono or polyfunctional carboxyl acids, carboxyl anhydrides and esters, ketones, ethers, alcohols, lactones, or phosphorous or organic silicon compounds . An example of a preferred titanium-based Ziegler-Natta catalyst is TiCl 3 -A1C1 3 • (n-propyl benzoate) , which is commercially available. However, most preferred catalysts for the copolymerization of propylene with 1-heptene or 1-nonene are titanium tetrachloride catalysts magnesium chloride supported, as hereinafter described. Thus, in the preferred catalysts, magnesium chloride is the catalyst support. The magnesium chloride may be used in the form of anhydrous magnesium chloride, or may have a water content between 0.02 mole of water/1 mole of magnesium chloride and 2 mole of water per 1 mole of magnesium chloride, ie it may be partially anhydrized. Most preferably, when the magnesium chloride is partially anhydrized, the water content of the magnesium chloride is, in one particular case, 1,5%, and, in a second particular case, 5% by mass. The magnesium chloride is preferably activated prior to contacting or loading it with the titanium tetrachloride. The activation of the magnesium chloride may be performed under inert conditions, i.e. in a substantially oxygen and water free atmosphere, and in the absence or in the presence of an inert saturated hydrocarbon liquid. Preferred inert saturated hydrocarbon liquids are aliphatic or cyclo-aliphatic liquid hydrocarbons, of which the most preferred are hexane and heptane. The magnesium chloride or support activation may be performed in two steps, designated (a x ) and (a 2 ) respectively. In step ( a λ ) , a complexing agent is added under inert conditions to a suspension of the magnesium chloride in the inert hydrocarbon liquid or to the magnesium chloride in powder form. The complexing agent may be selected from the class of an alcohol or a mixture of an alcohol and an ether. The alcohol may be a linear or branched alcohol with a total number of carbon atoms between 2 and 16. It is preferred to use a mixture of alcohols, with the most preferred being mixtures of linear and branched alcohols. When a linear alcohol is used, between 0,02 mole of alcohol/1 mole of magnesium chloride and 2 mole of alcohol/per 1 mole of magnesium chloride, may be used. When a branched alcohol or a mixture of linear and branched alcohols is used, between 0,015 mole alcohol/mole of magnesium chloride and 1,5 mole of alcohol/mole of magnesium chloride, may be used. The ether may be an ether with a total carbon number of 8 to 16. Either a single ether or a mixture of ethers can be used. When mixtures of linear alcohols and ethers are used, between 0,01 mole of alcohol/ether mixture per 1 mole of magnesium chloride and 2 mole of alcohol/ether mixture per 1 mole of magnesium chloride may be used. Most preferred are mixtures of branched alcohols and ethers, in which case between 0,015 mole of alcohol/ether mixture per 1 mole of magnesium chloride and 1.5 mole of alcohol/ether mixture per 1 mole of magnesium chloride, may be used. In the second step (a 2 ) , an alkyl aluminium compound is added, preferably in dropwise fashion, to the partially activated'magnesium chloride obtained in step (a x ) . Typical alkyl aluminium compounds which can be used are those expressed by the formula A1R 3 wherein R is an alkyl radical or radical component of 1 to 10 carbon atoms. Specific examples of suitable alkyl aluminium compounds that can be used are: tri-butyl aluminium, tri-isobutyl aluminium, tri- hexyl aluminium and tri-octyl aluminium. Preferred organo-aluminium compounds are diethylaluminium chloride, and tri-ethyl aluminium. The molar ratio of the alkyl aluminium compound to the anhydrous or partially anhydrized magnesium chloride initially used may be between 1:1 and 6:1. The preferred molar ratio of the alkyl aluminium compound to the magnesium chloride is 4:1 to 5:1. More particularly, the amount of the aluminium alkyl added to the partially activated magnesium chloride may comply with the equation: A > B + C + D where A represents total moles of aluminium alkyl, while B are mole of magnesium chloride, C are total moles of alcohol or ether /alcohol mixture and D are total moles of water (as the sum of total water present in the magnesium chloride and eventual traces of water in the solvent) . The loading of the activated magnesium chloride or support with the titanium tetrachloride may be performed in three steps, designated (b χ ) (b 2 )and (b 3 ) respectively. In the first step (b λ ) , to the support, after thorough washing thereof with hexane, is added, under stirring, a first ester component comprising an ester. The activated support may be in the form of a suspension in an inert saturated hydrocarbon liquid, as hereinbefore described. The ester may be selected from the class of organic esters derived from an aromatic acid, a diacid or an aromatic anhydride. The Applicant has surprisingly found that different performances of the catalyst are obtained if specific esters are used in this step of the catalyst preparation. Thus, preferred esters are esters derived from benzoic acid, phthalic acid and trimellitic anhydride. A particularly preferred ester is that where the ester is derived from a dibasic aromatic acid esterified with two different alcohols. In one version of this embodiment of the invention, a single ester may be used as a first ester component. In another version of this embodiment of the invention, a mixture of esters may be used as the first ester component. In an even more particular case, a tricomponent ester mixture may be used as the first ester component. The molar ratio of the first ester component to the initial magnesium chloride used may be between 0,05:1 and 5:1. The molar ratio between the two esters in a dicomponent mixture can be from 100:1 to 1:100. The molar ratio between the esters in a three component ester mixture can vary widely, but preferably is about 1:1:1. The stirring time may be between 1 min and 10 hours, preferably about 3 hours. The temperature during the stirring can be between 0°C and the lowest boiling point of any one of the esters in the multicomponent mixture or the inert saturated hydrocarbon liquid when used in this step of the catalyst preparation. In the second step (b 2 ) , titanium chloride, TiCl 4 , is added to the support/ester mixture, the resultant mixture or slurry stirred under reflux, and finally left to cool, e.g. for about 24 hours. The catalyst obtained may be thoroughly washed, e.g. with hexane. The molar ratio of TiCl 4 employed in this step to the initial magnesium chloride may be from about 2:1 to about 20:1, preferably about 10:1. In the third step (b 3 ) , a second ester component comprising an ester is added. In this step (b 3 ) , two cases can be distinguished, both surprisingly resulting in catalysts with different performances: i) The second ester component is the same as the first ester; ii) The second ester component is different to the first ester component. The Applicant has also surprisingly found that a very different family of catalysts may be obtained when a particular manner of the titanium chloride loading is used and which may lead to different and advantageous process performances when used in the different embodiments and versions of this invention. Thus, in one version of this embodiment of the invention, the order of loading of the titanium chloride may be: adding the titanium chloride to the activated support as in step (b 2 ) , followed by adding the electrodonor as in step (b ] _) , and followed by adding again the titanium chloride as in step (b 2 ) . Thus, the order of titanium chloride loading on the activated support is steps (b 2 ) - (b-_) - (b 2 ) . In this particular method of catalyst preparation, step (b λ ) and step (b 2 ) are followed by thorough washing with heptane at a temperature just below boiling. When a cocatalyst is employed in the polymerization it may, as stated hereinbefore, be an organo aluminium compound. Typical organo-aluminium compounds which can be used are compounds expressed by the formula AlR m X 3 _ m wherein R is a hydrocarbon component of 1 to 15 carbon atoms, X is a halogen atom, and m is an integer represented by 0 < m ≤ 3. Specific examples of suitable organo aluminium compounds that can be used are: a trialkyl aluminium, a trialkenyl aluminium, a partially halogenated alkyl aluminium, an alkyl aluminium sesquihalide, an alkyl aluminium dihalide. Preferred organo aluminium compounds are alkyl aluminium compounds, and the most preferred compound is triethylaluminium. The atomic ratio of aluminium to titanium in the catalyst system may be between 0,1:1 and 500:1, preferably between 1:1 and 100:1. For slurry phase copolymerization preferred slurrying or suspension agents are aliphatic or cyclo-aliphatic liquid hydrocarbons, with the most preferred being hexane and heptane . While the reaction temperature can be in the range of ambient to 300°C, it is preferably in the range of 50°C to 100°C, and most preferably in the range of 60°C to 90°C. While the pressure can be in the range of atmospheric pressure to 200kg/cm 2 , it is preferably in the range of 3kg/cm 2 to 30kg/cm 2 , still more preferably in the range of 4kg/cm 2 to 18kg/cm 2 . When using a catalyst prepared in accordance with the catalyst preparation process hereinbefore described, the parameters of the copolymerization reaction of propylene with 1-heptene or 1-nonene are thus such that the resultant copolymer of propylene with 1-heptene or 1-nonene is as hereinbefore described. The invention will now be described in more detail with reference to the following non-limiting examples. In these examples, the composition of the copolymers was determined by 13 C NMR. The following ASTM tests were used to determine the properties of the polymers in the examples: melt flow index - ASTM D 1238; tensile strength at yield - ASTM D 638 M; Young's modulus - ASTM D 638 M; hardness - ASTM D 2240; Izod impact strength - ASTM 256; density - ASTM D 1505; and hardness - ASTM D 2240. EXAMPLE 1 Catalyst A Preparation In a 250ml flask equipped with a reflux condenser and stirring facilities 2g of magnesium chloride with a total water content of 1,5% by mass was suspended in 60ml highly purified hexane. 4ml of a 1:1 molar mixture of dipentyl ether and ethanol were added to the flask, and the mixture stirred for 3 hours under reflux. The mixture was allowed to cool to ambient temperature, and lOg of tri-ethyl aluminium were added dropwise to avoid excessive heat build-up. The resultant slurry was allowed to cool to room temperature under stirring and then subjected to twelve washings using 50ml hexane each time, to obtain an activated support-containing slurry. To the activated support-containing slurry were added 2ml of a 1:1 molar mixture of ethanol and 1-nonanol, and the slurry stirred for 3 hours at ambient temperature. 15ml of TiCl 4 was then added, and the mixture stirred under reflux for 2 hours. After cooling down, the slurry was subjected to ten washing using 50ml hexane each time and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 0,2g of catalyst A and 10ml of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of 150mg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-nonene at 10 and 2,5g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depreεsurized and the catalyst deactivated by the addition of 100m isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,3 mol % 1-nonene and with a melt flow index of 1, 5dg/minute, was 105g. The polymer had the following properties: Tensile strength at yield 22,4 MPa Young' s modulus 967 MPa Hardness 61 Izod Impact strength 9 , 7 kJ/m 2 Density >0, 943g/cc EXAMPLE 2 Catalyst B Preparation In a 250m flask equipped with a reflux condenser and stirring facilities, 2g of magnesium chloride with a total water content of 1,5% by mass was suspended in 60m highly purified hexane. 4m of a 1:1 molar mixture of dipentyl ether and isopentanol were added to the flask, and the mixture stirred for 3 hours under reflux. The mixture was allowed to cool to ambient temperature, . and lOg of tri- ethyl aluminium were added dropwise to avoid excessive heat build-up. The resultant slurry was allowed to cool to room temperature under stirring and then subjected to twelve washings using 50m hexane each time, to obtain an activated support-containing slurry. To the activated support-containing slurry were added 2m of a 1:1 molar mixture of ethanol and 1-heptanol, and the slurry stirred for 3 hours at ambient temperature. 15m of TiCl 4 was then added, and the mixture stirred under reflux for 2 hours. After cooling down, the slurry was subjected to ten washing using 50m hexane each time and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 0,2g of catalyst B and 10m of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-nonene at 10 and 5g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100m isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,9 mol % 1-nonene and with a melt flow index 0,4dg/minute was 135g. The polymer had the following properties: Tensile strength at yield 17,7 MPa Young's modulus 535 MPa Hardness 51 Izod Impact strength 50,75 kJ/m 2 Density 0, 287g/cc EXAMPLE 3 Catalyst Al Preparation In a 250m flask equipped with a reflux condenser and stirring facilities, 2g of magnesium chloride with a total water content of 1,5% by mass was suspended in 60m£ highly purified hexane. 4m of ethanol were added to the flask, and the mixture stirred for 3 hours under reflux. The mixture was allowed to cool to ambient temperature, and lOg of tri-ethyl aluminium were added dropwise to avoid excessive heat build-up. The resultant slurry was allowed to cool to room temperature under stirring and then subjected to twelve washings using 50ml. hexane each time, to obtain an activated support-containing slurry. To the activated support-containing slurry were added 2m of a 1:1 molar mixture of ethanol and 1-nonanol, and the slurry stirred for 3 hours at ambient temperature. 15m of TiCl 4 was then added, and the mixture stirred under reflux for 2 hours. After cooling down, the slurry was subjected to ten washing using 50m hexane each time and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and. the temperature set at 85°C. A catalyst system, comprising 0,2g of catalyst Al and 10m of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-nonene at 10 and 7,5g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-nonene feeds were stopped and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100m isopropanol . The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,75 mol % 1-nonene with melt flow index 0 , 25dg/minute was 95g. The polymer had the following properties: Tensile strength at yield 15,25 MPa Young's modulus 675 MPa Hardness 53 Izod Impact strength 40,4 kJ/m 2 Density 0, 9305g/cc EXAMPLE 4 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 35 Og heptane and the temperature set at 85 °C. A catalyst system, comprising 0,2g catalyst B and 10m£ of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of 200mg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-nonene at 10 and lOg/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100m isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,3 mol % 1-nonene and with melt flow index 44dg/minute was 151g and the polymer had the following properties: Tensile strength at yield 5,5 MPa Young's modulus 370 MPa Hardness 32 Izod Impact strength 21,5 kJ/m 2 Density 0, 9232g/cc EXAMPLE 5 Catalyst Bl Preparation In a 250m flask equipped with a reflux condenser and stirring facilities, 2g of magnesium chloride with a total water content of 1,5% by mass was suspended in 60mt highly purified hexane. 4m£ of isopentanol were added to the flask and the mixture was stirred for 3 hours under reflux. The mixture was allowed to cool to ambient temperature, and lOg of tri-ethyl aluminium were added dropwise to avoid excessive heat build-up. The resultant slurry was allowed to cool to room temperature under stirring and then subjected to twelve washing using 50m hexane each time, to obtain an activated support-containing slurry. To the activated support-containing slurry were added 2ml? of a 1:1 molar mixture of ethanol and 1-heptanol, and the slurry stirred for 3 hours at ambient temperature. 15ml? of TiCl 4 was then added, and the mixture stirred under reflux for 2 hours. After cooling down, the slurry was subjected to ten washing using 50ml. hexane each time and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 0,2g catalyst Bl and 10ml? of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of 100 mg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-nonene at 10 and 8g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol . The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,1 mol % 1-nonene and with a melt flow index 2dg/minute was lOOg. The polymer had the following properties : Tensile strength at yield : 10 MPa Young's modulus 440 MPa Hardness 44 Izod Impact strength 55,3 kJ/m 2 Density 0, 925g/cc EXAMPLE 6 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 80°C. A catalyst system, comprising 0,2g of catalyst A and 10m of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-heptene at 10 and 6g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? iso propanol . The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,7 mol % 1- heptene and with a melt flow index 15dg/minute was 125g. The polymer had the following properties : Tensile strength at yield 9,22 MPa Young's modulus 483 MPa Hardness 42 Izod Impact strength 30,1 kJ/m 2 Density 0, 921g/cc EXAMPLE 7 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 80°C. A catalyst system, comprising 0,2g catalyst A and 10ml? of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-heptene at 10 and 4g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100m isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,3 mol % 1- heptene and with a melt flow index 18dg/minute, was 125g. The polymer had the following properties : Tensile strength at yield 11,1 MPa Young's modulus 572 MPa Hardness 45 Izod Impact strength 20,7 kJ/m 2 Density 0, 9261g/cc EXAMPLE 8 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 80°C. A catalyst system, comprising 0,2g of catalyst A and 10ml? of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-heptene at 10 and 2,5g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,7 mol % 1- heptene and with a melt flow index 17dg/minute was 115g. The polymer had the following properties : Tensile strength at yield 14,5 MPa Young's modulus 675 MPa Hardness 53 Izod Impact strength 8 , 5 kJ/m 2 Density 0, 9373g/cc EXAMPLE 9 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 80°C. The catalyst system, comprising 0,2g of catalyst A and 10ml? of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-heptene at 10 and l,5g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,45 mol % 1-heptene and with a melt flow index 28dg/minute was 115g. The polymer had the following properties: Tensile strength at yield 15, 8 MPa Young's modulus 924 MPa Hardness 55 Izod Impact strength 7,4 kJ/m 2 Density 0, 9420g/cc EXAMPLE 10 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 80°C. A catalyst system, comprising 0,2g of catalyst B and 10ml? of a 10% solution of tri-ethyl aluminium in heptane, was added and reacted under stirring in the presence of lOOmg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of ethylene and 1-heptene at 10 and 3g/min respectively were thereafter commenced. After 10 minutes the ethylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100m isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,0 mol % 1- heptene and with a melt flow index 48dg/minute was 12 Og. The polymer had the following properties: Tensile strength at yield 13,2 MPa Young's modulus 605 MPa Hardness 50 Izod Impact strength 13 kJ/m 2 Density 0, 933g/cc EXAMPLE 11 Catalyst C Preparation 20gm of partially anhydrized magnesium chloride with a water content of 1,5% by mass was stirred in 100ml? dibutyl ether at 80°C for 30 minutes. 200m ethanol were added, and the excess solvent from the resulting solution were removed under reduced pressure until crystallization occurred. This fine crystalline material was washed three times with 100ml? heptane. This activated support was then dried under reduced pressure. To the activated support thus formed was added 150m TiCl 4 in 100ml? heptane. The mixture was heated to 80°C and stirred for 60 minutes. This mixture was filtered while hot and washed with boiling heptane until no TiCl 4 could be detected in the washings. To the washed titanium containing compound was added 6g (1:0, lmg.Phthalate) of di-iso-butyl phthalate, heated to 80°C and stirred for 60 minutes. It was then filtered while hot and washed five times with boiling heptane. To this washed compound was added 150m TiCl 4 in 100m heptane, heated to 80°C and stirred for 60 minutes. The resultant catalyst was filtered while hot and washed with boiling heptane until no TiCl 4 could be detected in the washings, and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85 °C. A catalyst system, comprising 10ml? of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-nonene at 10 and l,5g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,9 mol % 1-nonene and with a melt flow index 2,3dg/minute was 50g. The polymer had the following properties: Tensile strength at yield 20,7 MPa Young' s modulus 937 MPa Hardness 61 Izod Impact strength 16 kJ/m 2 EXAMPLE 12 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 10m of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-nonene at 10 and 5g/min respectively were thererafter commenced. After 10 minutes the propylene and 1-nonene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml 1 isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,0 mol % 1-nonene and with a melt flow index 3,3dg/minute was 55g. The polymer had the following properties: Tensile strength at yield 20,1 MPa Young' s modulus 800 MPa Hardness 60 Izod Impact strength 18 kJ/m 2 EXAMPLE 13 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85 °C. A catalyst system, comprising 10ml? of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-nonene at 10 and 7,5g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-nonene feeds were stopped and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of lOOm isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,5 mol % 1-nonene and with a melt flow index 2,2dg/minute was 50g. The polymer had the following properties: Tensile strength at yield 16,5 MPa Young's modulus 546 MPa Hardness 56 Izod Impact strength 46, kJ/m 2 EXAMPLE 14 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen was added 350g heptane and the temperature set at 85 °C. A catalyst system, comprising 10m of a 10% solution of tri-ethyl aluminium in heptane, 1 , 5 2 of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-nonene at 10 and l,2g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-nonene feeds were stopped and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,2 mol % 1-nonene and with a melt flow index 2,4dg/minute was 70g. The polymer had the following properties: Tensile strength at yield 24,2 MPa Young's modulus 1014 MPa Hardness 65 Izod Impact strength 6 , 3 kJ/m 2 EXAMPLE 15 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85 °C. A catalyst system, comprising 10ml? of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-nonene at 10 and 6g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-nonene feeds were stopped and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,2 mol % 1-nonene and with a melt flow index 0 , 4dg/minute, was 50g. The polymer had the following properties: Tensile strength at yield 19,5 MPa Young' s modulus 850 MPa Hardness 57 Izod Impact strength 29,5 kJ/m 2 EXAMPLE 16 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen was added 350g heptane and -the temperature set at 85 °C. A catalyst system, comprising 10m of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-heptene at 10 and l,6g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 0,4 mol % 1- heptene and with a melt flow index lldg/minute was 70g. The polymer had the following properties: Tensile strength at yield 23,1 MPa Young' s modulus 885 MPa Hardness 61 Izod Impact strength 6 kJ/m 2 EXAMPLE 17 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85 °C. A catalyst system, comprising 10m of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-heptene at 10 and 2,5g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,0 mol % 1- heptene and with a melt flow index 13dg/minute was 75g. The polymer had the following properties: Tensile strength at yield 18,2 MPa Young' s modulus 745 MPa Hardness 58 Izod Impact strength 10 kJ/m 2 EXAMPLE 18 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 10m of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-heptene at 10 and 4g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,4 mol % 1- heptene and with a melt flow index lOdg/minute was 65g. The polymer had the following properties: Tensile strength at yield : 15,1 MPa Young's modulus 546 MPa Hardness 56 Izod Impact strength 19 kJ/m 2 EXAMPLE 19 To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 350g heptane and the temperature set at 85°C. A catalyst system, comprising 10ml? of a 10% solution of tri-ethyl aluminium in heptane, 1,5ml? of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst C, was introduced in that order and reacted under stirring for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-heptene at 10 and 6g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 2 mol % 1-heptene and with a melt flow index 5dg/minute was 65g. The polymer had the following properties: Tensile strength at yield 12, 6 MPa Young' s modulus 372 MPa Hardness 50 Izod Impact strength 46,5 kJ/m 2 EXAMPLE 20 Catalyst D Preparation Partially anhydrized magnesium chloride (20g) was stirred in 100m dibutyl ether at 80°C for 30 minutes. 2 00m£ ethanol were added, and the excess solvent from the resulting solution removed under reduced pressure until crystallization occurred. This fine crystalline material was washed three times with 100m heptane. This activated support was then dried under reduced pressure. To the activated support thus formed was added 6g (1:0, lmg:Phthalate) of di-iso-butyl phthalate . The mixture was heated to 80°C and stirred for 60 minutes. It was then filtered while hot and washed five times with boiling heptane. 150m TiCl 4 in 100m heptane was then added. The mixture was heated to 80°C and stirred for 60 minutes. This mixture was filtered while hot and washed with boiling heptane until no TiCl 4 could be detected in the washings. To the washed titanium containing compound was added 6g (1:0, lmg: Phthalate) of di-iso-butyl phthalate. The mixture was heated to 80°C and stirred for 60 minutes. It was then filtered while hot and washed five times with boiling heptane, and then dried. Copolymerization To a thoroughly cleaned 1 litre autoclave fitted with stirring and heating/cooling facilities and flushed with nitrogen, was added 35Og heptane and the temperature set at 85°C. A catalyst system, comprising 10ml? of a 10% solution of tri-ethyl aluminium in heptane, l,5m of a 7% solution of di-isopropyl dimethoxy silane in heptane and 0,3g of catalyst D, was introduced in that order and reacted under stirring in the presence of 20mg hydrogen for 5 minutes to activate the catalyst. Simultaneous flows of propylene and 1-heptene at 10 and 5g/min respectively were thereafter commenced. After 10 minutes the propylene and 1-heptene feeds were stopped, and the reaction continued for another 50 minutes. The reactor was depressurized and the catalyst deactivated by the addition of 100ml? isopropanol. The slurry was filtered and the polymer washed with acetone and dried under vacuum at 80°C. The yield of copolymer containing 1,75 mol % 1-heptene and with a melt flow index 45dg/minute was 70g. The polymer had the following properties: Tensile strength at yield 13,5 MPa Young's modulus 450 MPa Hardness 53 Izod Impact strength 19,8 kJ/m 2

Claims: CLAIMS 1. A polymer obtained from a first olefin having fewer than 4 carbon atoms, and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99, 9:0,1. 2. A polymer which comprises a polymerization product obtained by polymerizing at least a first olefin having fewer than 4 carbon atoms and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99, 9:0, 1. 3. A polymer according to Claim 1 or Claim 2, which is a copolymer of the first olefin and the second olefin. 4. A copolymer of a first olefin having fewer than 4 carbon atoms, and a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, with the molar proportion of the first olefin to the second olefin in the polymer being from 90:10 to 99, 9:0,1. 5. A copolymer according to Claim 3 or Claim 4, wherein the second olefin is 1-heptene, 1-nonene, or 1- undecene. 6. A copolymer according to Claim 5, which has a) a melt flow index, as measured according to ASTM D 1238, in the range of 0,01 to 50dg/min ; and b) an Izod notched impact strength, as measured according to ASTM D 256, greater than 5 kJ/m 2 ; and/or c) a tensile strength at yield, as measured according to ASTM D 638 M, greater than 5 MPa; and/or d) a modulus, as measured according to ASTM D 638 M, greater than 100 MPa. 7. A copolymer according to any one of Claims 3 to 6 inclusive, which is that obtained by reacting the first olefin and the second olefin in one or more reaction zones, while maintaining in the reaction zone(s) a pressure in the range between atmospheric and 200 kg/cm 2 and a temperature between ambient and 300°C, in the presence of a Ziegler-Natta catalyst or catalyst system. 8. A copolymer according to any one of Claims 3 to 7 inclusive, wherein the first olefin is ethylene, and wherein the polymer has a density, as measured according to ASTM D 1505, in the range of 0,910 to 0,950g/cm 3 . 9. A copolymer according to Claim 8 , wherein the second olefin is 1-heptene, with the molar proportion of ethylene to 1-heptene being from 98:2 to 99,8:0,2, and with the polymer having a) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 10 [C 7 ] where [C 7 ] is the molar concentration of 1-heptene in the polymer; and/or b) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -4.4 [C 7 ] + 17 ; and/or c) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -275 [C 7 ] + 850 ; and/or d) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -10 [C 7 ] + 56 10. A copolymer according to Claim 8, wherein the second olefin is 1-nonene, with the molar proportion of ethylene to 1-heptene being from 98,5:1,5 to 99,9:0,1, and with the polymer having a) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 13,3[C 9 ] where [C 9 ] is the molar concentration of 1-nonene in the polymer; and/or b) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -16.67 [C 9 ] + 25 ; and/or c) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -666.67 [C 9 ] + 1100 ; and/or d) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -30 [C 9 ] + 65 11. A copolymer according to any one of Claims 3 to 7 inclusive, wherein the first olefin is propylene, the second olefin is 1-heptene, with the molar proportion of propylene to 1-heptene being from 98,0:2,0 to 99,8:0,2, and the polymer has a) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 7.5 [C 7 ] where [C 7 ] is the molar concentration of 1-heptene in the polymer; and/or b) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: σ > -7[C 7 ] + 24 ; and/or c) a modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -350 [C 7 ] + 1000 ; and/or d) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -7.2 [C 7 ] + 63 12. A polymer according to any one of Claims 3 to 7 inclusive, wherein the first olefin is propylene, the second olefin is 1-nonene, with the molar proportion of propylene to 1-nonene being from 98,5:1,5 to 99,9:0,1, and the polymer has a) an Izod notched impact strength, I, as measured according to ASTM D 256, which complies with the following equation: I > 15 [C 9 ] where [C g ] is the molar concentration of 1-nonene in the polymer; and/or b) a tensile strength at yield, σ, as measured according to ASTM D 638 M, which complies with the following equation: a > -5.3 [C 9 ] + 24 ,- and/or c) A modulus, E, as measured according to ASTM D 638 M, which complies with the following equation: E > -333.3 [C 9 ] + 1000 ; and/or d) a hardness, H, as measured according to ASTM D 2240, which complies with the following equation: H > -6.67[C 9 ] + 65 13. A process for producing a polymer, which process comprises reacting a reaction mixture comprising, as a first monomer, a first olefin having fewer than 4 carbon atoms and, as a second monomer, a second olefin having a total number of carbon atoms greater than 5 and having an uneven number of carbon atoms, in one or more reaction zones, while maintaining the reaction zone(s) at a pressure between atmospheric pressure and 200kg/cm 2 , and at a temperature between ambient and 300°C, in the presence of a catalyst system or a catalyst system comprising a catalyst and a cocatalyst, such that the molar proportion of the first olefin to the second olefin in the resultant polymer is from 98:10 to 99,8:0,2. 14. A process according to Claim 13, wherein the first olefin is ethylene while the second olefin is 1- heptene or 1-nonene, with the catalyst being a magnesium chloride supported titanium tetrachloride catalyst . 15. A process according to Claim 14, wherein the catalyst is that obtained by activating an anhydrous or partially anhydrized magnesium chloride support by (i) adding a complexing agent under inert conditions to a suspension of the magnesium chloride in an inert saturated hydrocarbon liquid, or to the magnesium chloride in powder form, with the complexing agent comprising a mixture of at least one branched alcohol having between 2 and 16 carbon atoms and at least one ether having between 8 and 16 carbon atoms, with sufficient of the complexing agent mixture being used so that the molar proportion of mixture to magnesium chloride is from 0,05:1 to 1,5:1, to obtain partially activated magnesium chloride ; and (ii) adding an alkyl aluminium compound to the partially activated magnesium chloride, with sufficient alkyl aluminium compound being used so that the molar ratio of the alkyl aluminium compound to the magnesium chloride is from 1:1 to 6:1, thereby to obtain activated magnesium chloride; loading the activated magnesium chloride with titanium chloride by (i) adding to the magnesium chloride a dicomponent alcohol mixture, with one alcohol in the mixture having the same number of carbon atoms as the first monomer and the other alcohol having the same number of carbon atoms as the second monomer, and with the molar ratio of the alcohol mixture to the initial magnesium chloride used being between 0,4:1 and 4:1, and (ii) adding titanium chloride to the magnesium chloride/alcohol mixture, with the molar ratio of titanium chloride to initial magnesium used being from 2:1 to 20:1. 16. A process according to Claim 13, wherein the first olefin is propylene while the second olefin is 1- heptene or 1-nonene, with the catalyst being a magnesium chloride supported titanium tetrachloride catalyst. 17. A process according to Claim 16, wherein the catalyst is that obtained by activating an anhydrous or partially anhydrized magnesium chloride support by (i) adding a complexing agent under inert conditions to a suspension of the magnesium chloride in an inert saturated hydrocarbon liquid, or to the magnesium chloride in powder form, with the complexing agent comprising a mixture of at least one branched alcohol having between 2 and 16 carbon atoms and at least one ether having between 8 and 16 carbon atoms, with sufficient of the complexing agent mixture being used so that the molar proportion of mixture to magnesium chloride is from 0,015:1 to 1,5:1, to obtain partially activated magnesium chloride, and (ii) adding an alkyl aluminium compound to the partially activated magnesium chloride, with sufficient alkyl aluminium compound being used so that the molar ratio of the alkyl aluminium compound to the magnesium chloride is from 1:1 to 6:1, thereby to obtain activated magnesium chloride; and loading the activated magnesium chloride with titanium chloride by (i) adding a first ester component comprising an ester or a mixture of esters, to the activated magnesium chloride, with the molar ratio of the first ester component to the initial magnesium chloride used being between 0,05:1 and 5:1; (ii) thereafter adding titanium chloride to the magnesium chloride/ester mixture, with the molar ratio of titanium chloride to initial magnesium chloride used being from 2:1 to 20:1; and (iii) adding a second ester component comprising an ester or a mixture of esters to the titanium chloride containing magnesium chloride/ester mixture. 18. A process according to Claim 18 wherein, in the production of the catalyst, the first ester component is the same as the second ester component . 19. A process according to Claim 17, wherein, in the production of the catalyst, the first and second ester components are different. 20. A process according to Claim 16, wherein the catalyst is that obtained by activating an anhydrous or partially anhydrized magnesium chloride support by (i) adding a complexing agent under inert conditions to a suspension of the magnesium chloride in an inert saturated hydrocarbon liquid, or to the magnesium chloride in powder form, with the complexing agent comprising a mixture of at least one branched alcohol having between 2 and 16 carbon atoms and at least one ether having between 8 and 16 carbon atoms, with sufficient of the complexing agent mixture being used so that the molar proportion of mixture to magnesium chloride is from 0,015:1 to 1,5:1, to obtain partially activated magnesium chloride, and (ii) adding an alkyl aluminium compound to the partially activated magnesium chloride, with sufficient alkyl aluminium compound being used so that the molar ratio of the alkyl aluminium compound to the magnesium chloride is from 1:1 to 6:1, thereby to obtain activated magnesium chloride; and loading the activated magnesium chloride with titanium chloride by (i) adding titanium chloride to the activated magnesium chloride, with the molar ratio of titanium chloride to initial magnesium chloride used being from 2:1 to 20:1; (ii) adding an ester component comprising an ester or a mixture of esters to the titanium containing magnesium chloride, with the molar ratio of the ester component to the initial magnesium chloride used being between 0,015:1 and 5:1; and (iii) adding titanium chloride to the titanium containing magnesium chloride/ester mixture, with the molar ratio of titanium chloride added in this step to the initial magnesium chloride used being from 2:1 to 20:1. 21. A process according to any one of Claims 14 to 20 inclusive, wherein a catalyst system is used, with the cocatalyst being an organo aluminium compound, and sufficient of the cocatalyst being used such that the atomic ratio of aluminium to titanium in the catalyst system is from 0,1:1 to 500:1. 22. A novel polymer, substantially as described and exemplified herein, . 23. A novel process for producing a polymer, substantially as described and exemplified herein.

Inventors: JOUBERT DAWID JOHANNES, POTGIETER IGNATIUS HENDRIK, TINCUL IOAN, YOUNG DESMOND AUSTIN, JOUBERT, DAWID, JOHANNES, POTGIETER, IGNATIUS, HENDRIK, TINCUL, IOAN, YOUNG, DESMOND, AUSTIN
Applicants: JOUBERT DAWID JOHANNES, POTGIETER IGNATIUS HENDRIK, SASOL CHEMICALS EUROP LTD, SASOL TECH PTY LTD, TINCUL IOAN, YOUNG DESMOND AUSTIN, JOUBERT, DAWID, JOHANNES, POTGIETER, IGNATIUS, HENDRIK, SASOL CHEMICALS EUROPE LIMITED, SASOL TECHNOLOGY (PROPRIETARY) LIMITED, TINCUL, IOAN, YOUNG, DESMOND, AUSTIN
Application year: 1999
Main classification: C08F210
IPC codes: C08F4, C08F210