EP0000997B1 - Compositions à base de trichlorure de titane, préparation de celles-ci, système catalytique les contenant et polymérisation des oléfines à l'aide de ce système - Google Patents

Compositions à base de trichlorure de titane, préparation de celles-ci, système catalytique les contenant et polymérisation des oléfines à l'aide de ce système Download PDF

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EP0000997B1
EP0000997B1 EP78300283A EP78300283A EP0000997B1 EP 0000997 B1 EP0000997 B1 EP 0000997B1 EP 78300283 A EP78300283 A EP 78300283A EP 78300283 A EP78300283 A EP 78300283A EP 0000997 B1 EP0000997 B1 EP 0000997B1
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compound
product
temperature
titanium trichloride
propylene
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EP0000997A1 (fr
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Ashley Dormer Bye
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Imperial Chemical Industries Ltd
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Imperial Chemical Industries Ltd
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/06—Phosphorus compounds without P—C bonds
    • C07F9/08—Esters of oxyacids of phosphorus
    • C07F9/09—Esters of phosphoric acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/06—Phosphorus compounds without P—C bonds
    • C07F9/08—Esters of oxyacids of phosphorus
    • C07F9/141—Esters of phosphorous acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/28—Phosphorus compounds with one or more P—C bonds
    • C07F9/50—Organo-phosphines
    • C07F9/5045—Complexes or chelates of phosphines with metallic compounds or metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
    • C07F9/02—Phosphorus compounds
    • C07F9/28—Phosphorus compounds with one or more P—C bonds
    • C07F9/50—Organo-phosphines
    • C07F9/53—Organo-phosphine oxides; Organo-phosphine thioxides
    • C07F9/5345—Complexes or chelates of phosphine-oxides or thioxides with metallic compounds or metals

Definitions

  • the present invention relates to transition metal compositions, the preparation of such compositions and the use of such compositions as a component of a catalyst system for the polymerisation of olefine monomers.
  • the polymerisation of olefine monomers using the so-called Ziegler-Natta catalysts has been known for a number of years. These catalysts comprise a compound of a transition metal together with an organic compound of a non-transition metal. There have been many proposals to improve the activity and/or stereospecificity of the catalyst system by the use of additional catalyst components or by modifying either the transition metal compound or the non-transition metal compound.
  • the transition metal compound is titanium trichloride which is activated by copulverising with an additive which is at least one specified organic compound, or a reaction product, complex or mixture of an aluminium trihalide and the at least one specified organic compound which may be an ether and/or a phosphorus compound.
  • a modified transition metal composition is prepared by reacting a transition metal compound, for example titanium tetrachloride, with an organo-metallic compound, for example an alkyl aluminium halide, and thereafter heating the solid reaction product with at least one specified organic sulphur-containing compound.
  • This specification also discloses the preparation of copolymers of propylene and ethylene having improved properties.
  • French specification 2 320 308 there is described a titanium trichloride material having a specified X-ray diffraction pattern and which includes a complexed monoether or polyether.
  • the titanium trichloride material of French specification 2 320 308 is obtained by reducing titanium tetrachloride with an organo-aluminium compound, optionally heat treating the reduction product, heating the product in the presence of the monoether or polyether and thereafter washing the heated product. There is no suggestion of using a material in addition to the monoether or polyether.
  • the group R is conveniently a hydrocarbyl group containing from 1 up to 20 carbon atoms and may be an alkyl, aryl, cycloalkyl, alkaryl or aralkyl group. Typically, the group R is an alkyl group containing from 2 up to 10 carbon atoms, for example an ethyl or butyl group.
  • X is chlorine and the value of x is such that 0 ⁇ x ⁇ 2.00 and is especially about one.
  • n is preferably greater than 0 and less than 0.3, especially greater than 0 and less than 0.2.
  • the ether or thioether which is E is a monoether, polyether, monothioether or polythioether which is capable of forming coordination complexes or compounds with aluminium halides or aluminium alkyls, these complexes or compounds being soluble in at least one of the solvents selected from the monoether, polyether, monothioether and polythioether themselves, aromatic and aliphatic hydrocarbons and the halogen-containing derivatives thereof.
  • the polyether and the polythioether contain at least two ether groups or at least two thioether groups respectively.
  • the ether or thioether may be a compound of the type R I- Z-R I where R' and R 2 , which may be the same or different, are hydrocarbyl groups containing 1 up to 12 carbon atoms; and Z is an oxygen or a sulphur atom.
  • R 1 and R 2 are conveniently the same and may be alkyl, aryl, alkaryl, aralkyl or cycloalkyl groups. It is preferred that R 1 and R 2 are phenyl groups or particularly alkyl groups containing from 4 up to 6 carbon atoms.
  • Polyethers which may be used as the compound E include 1-methoxy-2-(!3-methoxyethoxy)ethane and 1,2-diphenoxyethane. It is especially preferred that E is di-n-butyl ether or di-isoamyl ether.
  • the compound L is a phosphorus-containing Lewis Base compound such as an organic phosphine or an organic phosphine oxide or a derivative thereof.
  • Organic phosphorus-containing Lewis Base compounds which are suitable for use as components of olefine polymerisation catalysts, and which may be used as the compound L, are disclosed, inter alia, in British Patent Specifications 803 198; 920118; 921 954; 1017977; 1049723; 1122010; 1150845; 1208815; 1 234 657; 1 324 173; 1 359 328; 1 383 207; 1 423 658; 1 423 659 and 1 423 660.
  • the compound L is conveniently a compound of the general formula: where
  • R 4 and R 5 are hydrocarbyl, or hydrocarbyloxy, groups, for examples as in tri-n-butyl phosphine, triphenyl phosphine, tri-n-butyl phosphine oxide, trioctyl phosphine oxide, triphenyl phosphine oxide, tri-n-butyl phosphite, triphenyl phosphite, tris(nonylphenyl)phosphite, triethyl phosphate, tri-n-butyl phosphate and triphenyl phosphate.
  • a and b need not be the same and typically will be different.
  • the value of a is conveniently from 0.01 up to 0.2 and the value of b is conveniently from 0.005 up to 0.20.
  • composition of matter in accordance with the present invention has the formula: where
  • the composition of matter has a relatively low specific surface area.
  • the specific surface area is typically less than 50 m 2 /g and especially from 1 up to 30 m 2 /g.
  • the term "specific surface area” as used herein is the surface area of one gramme of the product, the surface area having been measured using the technique of BS 4359/1.
  • the colour of the composition of matter may be from violet to brown and the composition of matter is typically a reddish-brown in colour.
  • the X-ray diffraction spectrum is that of the beta-form of titanium trichloride, but lines which are characteristic of the layer lattice forms [for example a line corresponding to a lattice spacing of about 0.59 nm (5.9A)] have also been observed in the spectrum of some compositions of matter in accordance with the present invention.
  • the reduction product may be subjected to a thermal treatment at a temperature in the range from 40°C up to 130°C for a period of from 5 minutes up to 20 hours, and the thermally treated product may then be subjected to stage 2) of the process.
  • the product may be subjected to an additional treatment in which an aluminium alkyl compound, typically diethyl aluminium chloride, is added, followed by an olefine monomer; typically propylene, conveniently in an amount of 0.1 up to 2.0 grammes for each gramme of the titanium trichloride-containing product.
  • an aluminium alkyl compound typically diethyl aluminium chloride
  • an olefine monomer typically propylene
  • the various stages of the preparation of the titanium trichloride-containing product are preferably effected in the presence of a suitable inert hydrocarbon liquid which is stirred.
  • This hydrocarbon liquid is conveniently an aliphatic or cycloaliphatic hydrocarbon such as hexane, heptane, decane or dodecane or mixtures thereof.
  • Suitable reducing agents include organic aluminium compounds of the general formulae wherein
  • the reducing agent is an organic aluminium compound, it is conveniently one in which the value of x' is from 1.5 up to 2.0. However, satisfactory products may be obtained when x' has a value of 3.0.
  • the organic aluminium compound may be aluminium triethyl or more preferably diethyl aluminium chloride or ethyl aluminium sesquichloride.
  • the reduction of the titanium tetrachloride is preferably carried out at a temperature which is below about 80°C.
  • the temperature used depends on the particular reducing agent which is used. Thus, if the reducing agent is an alkyl aluminium sesquihalide, it is preferred to carry out the reduction at a temperature of between -20°C and +20°C, very conveniently at 0°C. If the reducing agent is a dialkyl aluminium halide, whilst the temperature may be lower, for example as low as -40°C, satisfactory products can be obtained by using temperatures in the same range, that is temperatures in the range from -20°C up to +20°C, although temperatures of -40°C up to +10°C are particularly suitable.
  • the reducing agent is an aluminium trialkyl, or an organic aluminium hydride
  • lower reduction temperatures are preferred, particularly temperatures from -100°C up to 0°C, especially about -70°C up to about -40°C.
  • the reducing agent is an alkyl aluminium dihalide the preferred reduction temperatures are in the range from 0°C up to 40°C, especially from 10°C up to 30°C.
  • the reduction may be effected at a temperature of from -80°C up to +80°C, conveniently in the range from 0°C up to 40°C.
  • the quantity of the reducing agent depends on the particular reducing agent which is used. Using an organic aluminium compound the proportion used is typically from 0.1 up to 2.0 moles of the organic aluminium compound for each mole of titanium tetrachloride. Using a dialkyl aluminium halide, or a material such as an aluminium sesquihalide which may be regarded as containing a proportion of a dialkyl aluminium halide, the preferred proportions of the organic aluminium compound are from 0.5 up to 1.5 moles of dialkyl aluminium halide for each mole of titanium tetrachloride. Using an aluminium trialkyl the preferred proportions are less and are typically in the range from 0.25 up to 0.5 moles for every mole of titanium tetrachloride. Using a compound of the type TiCl,.2AICI,.arene, it is preferred to use equimolar proportions of the two reactants or an excess quantity of titanium tetrachloride.
  • stage 1 of the process is a solid which may be separated from the reaction medium and washed several times and finally resuspended in a sample of fresh hydrocarbon liquid.
  • stage 2) or the optional thermal treatment stage is effected in the presence of the liquid reaction medium from stage 1) when the reducing agent is an organic aluminium compound.
  • the reduction product is preferably heated to a temperature of at least 60°C.
  • the time of heating is dependent on the temperature used and shorter times are preferably used at higher temperatures. It is preferred that the conditions of temperature and time are such that the heated product contains a small proportion of the layer lattice structure as shown by the X-ray diffraction pattern of this material.
  • the heated product is separated from the reaction medium and washed several times before effecting stage 2).
  • the compounds E and L may be added simultaneously or sequentially and, in the latter case, the compounds E and L may be added in eithers order. It is preferred that the compound E and the compound L are added separately and particularly useful results have been obtained when the compound E has been added first.
  • the contacting of the reduction product with the compounds E and L may be effected by adding one, or both, of the compounds to a stirred suspension of the reduction product at ambient temperature and then heating the mixture to the temperature of at least 60°C. However, it is preferred to heat the reduction product to the temperature of at least 60°C and then add one, or both, of the compounds E and L to the heated material. It is not necessary to contact the reduction product at a temperature of at least 60°C with both compound E and compound L, since satisfactory results have been obtained by contacting the reduction product with only one of compound E or compound L at the temperature of at least 60°C and thereafter contacting the reduction product with the other compound at a temperature below 60°C such as ambient temperature. It is however preferred to heat the reduction product, which may have been subjected to the optional thermal treatment, to the temperature of at least 60°C, and, whilst maintaining that temperature, add first the compound E and thereafter the compound L.
  • the contacting with compound E or compound L may be repeated and using such a procedure the reduction product is preferably separated from the reaction mixture and washed before repeating the contacting with compound E or compound L.
  • Contacting with compounds E and L may be effected in more than one step, for example by repeating the contacting with at least one of the compounds E or L.
  • a first contacting step may be effected with one of the compounds E and L, and a further and separate contacting step is then effected with the other one of compounds E and L. If contacting is effected in more than one step, it may be sufficient to wash the product between the contacting steps and washing after the final contacting step may not be necessary. However, it will be appreciated that such a procedure is possible only if washing is effected after contacting with compound E and thereafter the final contacting step is effected without the addition of any of the compound E.
  • a convenient technique for effecting such a procedure is to heat the product of stage 1) to the temperature of at least 60°C, add compound E to the heated product some time after the desired temperature has been attained, for example 30 minutes to two hours after attaining the desired temperature, wash the heated product, heat the washed product to the temperature of at least 60°C and add compound L at any time after attaining the desired temperature.
  • stage 2 the contacting with compounds E and L, is effected in a single step, then the final stage of the process is to wash the product of stage 2).
  • stage 2 it is not necessary to subject the titanium trichloride product to a final washing stage provided that the titanium trichloride product is not contacted with compound E after the final washing stage.
  • washing can be effected at various stages of the process, the only necessary washing stage is subsequent to the contacting, or the final contacting, with the compound E.
  • the amount of the compound E which is used is preferably from 0.5 up to 3.0 moles for every mole of titanium trichloride present in the reduction product and it is particularly preferred to use between 0.8 and 2.5 moles per mole of titanium trichloride present in the reduction product.
  • the amount of the compound L which is used is conveniently in the range from 0.01 up to 2.0 moles for each mole of titanium trichloride present in the reduction product. It is particularly preferred to use from 0.01 up to 0.5 mole of the compound L, especially from 0.02 up to 0.2 mole of the compound L.
  • the temperature at which the contacting of the reduction product with the compound E and/or the compound L is effected is at least 60°C and may be up to 150°C. It is preferred to use temperatures of at least 80°C and not more than 130°C. Especially preferred temperatures are in the range from 90°C up to 120°C.
  • the heating time is preferably at least one hour and conveniently does not exceed 20 hours, particularly at least 2 hours and not more than 10 hours.
  • compounds E and L are added to the reduction product at the temperature of at least 60°C, and the reduction product has been subjected to optional thermal treatment stage, it is preferred that at least one of the compounds E or L is added as soon as the reduction product attains the desired temperature. If compounds E and L are added separately in a single step, the second of the two compounds is conveniently added 5 minutes to two hours, for example 30 minutes, after the addition of the first of the two compounds.
  • the new composition of matter of the present invention may be used as one component of an olefine polymerisation catalyst.
  • an olefine polymerisation catalyst comprising: 1) a titanium trichloride-containing material of the type hereinbefore described; and 2) at least one compound of aluminium, or of a non-transition metal of Group IIA of the Periodic Table, or a complex of an organo-metallic compound of a non-transition metal of Group IA or Group IIA of the Periodic Table with an organo-aluminium compound.
  • Periodic Table referred to herein is the Short Periodic Table as set out inside the back cover of "General and Inorganic Chemistry" by J. R. Partington, Second Edition, published by MacMillan and Company Limited, London in 1954.
  • the organo-metallic component which is component 2) of the catalyst can be a Grignard reagent which is substantially ether-free or a compound such as diphenyl magnesium.
  • this component can be a complex of an organo-metallic compound of a non-transition metal of Groups IA or IIA with an organo-aluminium compound, for example Mg[AI(C 2 H,),], or lithium aluminium tetraalkyl.
  • component 2) is an organo-aluminium compound such as a hydrocarbyl aluminium sulphate, a hydrocarbyl oxyhydrocarbyl aluminium, or particularly a trihydrocarbyl aluminium or dihydrocarbyl aluminium halide or hydride, especially triethylaluminium or diethylaluminium chloride since catalysts including triethylaluminium give a high polymerisation rate whilst catalysts including diethylaluminium chloride give a relatively high percentage yield of the desirable insoluble (isotactic) polymer.
  • a mixture of compounds can be used if desired, for example, a mixture of a trialkyl aluminium and a dialkyl aluminium halide. It may be preferred to use catalysts giving a low level of residual halogen in the polymer product in which case the organo-metallic component is desirably a halogen- free compound, particularly a trihydrocarbyl aluminium.
  • the catalyst can also contain, in addition to components 1) and 2), a further component, component 3), which is an organo-Lewis Base compound.
  • This can be any Lewis Base which is effective to alter the activity and/or stereospecificity of a Ziegler catalyst syste.
  • Lewis Bases have such an effect and these include compounds containing phosphorus and/or nitrogen atoms, oxygen compounds such as ethers, ester, ketones, and alcohols, and their sulphur-containing analogues, silicon compounds such as silanes and siloxanes, sulphones, sulphonamides and fused-ring heterocyclic sulphur compounds.
  • Catalysts containing organo-Lewis Base compounds, or complexes including organo-Lewis Base compounds are disclosed, inter alia, in British Patent Specifications 803 198; 809 717; 880 998; 896 509; 920 118; 921 954; 933 236; 940 125; 966025; 969074; 971 248; 1 013 363; 1 017 977; 1 049 723; 1 122 010; 1 150845; 1 208 815; 1 234657; 1 324 173; 1 359 328; 1 383 207; 1 423 658; 1 423 659 and 1 423 660; Belgian Patent Specification 693 551; and published German Patent Application 2 600 552.
  • organo-Lewis Base compound a Lewis Base which contains at least one atom of sulphur, nitrogen and/or phosphorus.
  • organo-Lewis Base compounds which can be used as the optional component 3) of the catalyst, include sulphur compounds such as diphenylsulphone, secondary or tertiary amines such as dibutylamine or tributylamine, diamines such as N,N,N',N'-tetramethylethylenediamine, and compounds which include both phosphorus and nitrogen atoms, such as hexamethylphosphoric triamide; N,N,N',N'-tetramethylethyl phosphorodiamidate; N,N,N',N',N"-pentamethyl-N"- ⁇ -- dimethylaminoethylphosphoric triamide; 2-dimethylamino-1,3-dimethyl-1,3,2-diaza-phospholidine-2- oxide and octa
  • the catalyst may also include a substituted or unsubstituted polyene (component 4)), which may be an acrylic polyene such as 3-methyl-heptatriene (1,4,6) or a cyclic polyene such as cyclooctariene, cyclooctatetraene or cycloheptatriene or derivatives of the cyclic polyenes such as the alkyl- or alkoxy- substituted cyclic polyenes; tropylium salts or complexes, tropolone or tropone.
  • a substituted or unsubstituted polyene component 4
  • the catalyst may also include a substituted or unsubstituted polyene (component 4)), which may be an acrylic polyene such as 3-methyl-heptatriene (1,4,6) or a cyclic polyene such as cyclooctariene, cyclooctatetraene or cycloheptatriene or derivatives of the cyclic polyenes
  • the proportions of the various catalyst components can be carried widely depending both on the materials used and the absolute concentrations of the components.
  • each gramme atom of the transition metal which is present in component 1) of the catalyst there is present at least 0.05, and preferably at least 1.0, and if desired as many as 50 or even more, moles of component 2).
  • a Lewis Base is included, then for each mole of the transition metal compound there is conveniently present from 0.01 up to 10, preferably from 0.1 up to 4, moles of the Lewis Base, provided that the amount of Lewis Base is less than the amount of component 2).
  • any polyene which is present, plus any Lewis Base should preferably, in total number of moles, be less than the number of moles of component 2).
  • the number of moles of polyene is conveniently in the range 0.01 up to 1.0, especially 0.05 up to 0.5, for example from 0.1 up to 0.2. If both Lewis Base and polyene are included, these can conveniently be used in equimolar proportions but the relative proportions of these components may be varied to give the optimum results.
  • the catalysts of the present invention are particularly suitable for the polymerisation and copolymerisaion of olefine monomers by contacting at least one olefine monomer with a catalyst of the type hereinbefore defined.
  • a process for the production of a polymer or copolymer of an olefine monomer wherein at least one olefine monomer (including ethylene) is polymerised by contacting the at least one olefine under polymerisation conditions with an olefine polymerisation catalyst as hereinbefore defined.
  • Monomers which can be polymerised by the present process include butene-1, and 4-methylpentene-1 and particularly propylene. These olefines may be copolymerised together or preferably may be copolymerised with ethylene, conveniently using a sequential polymerisation process such as is described in British Patents 970 478; 970 479 and 1 014944.
  • component 1) of the catalyst system contains some titanium trichloride in the betaform, it has been found that the process of the present invention can be used for the polymerisation of propylene to give a relatively low proportion of the undesirable soluble polymer. Furthermore, many of the catalyst systems give a high rate of polymerisation.
  • Polymerisation can be carried out in the known manner, for example in the presence or absence of an inert diluent such as a suitably purified paraffinic hydrocarbon, in the liquid phase using excess liquid monomer or in the gaseous phase.
  • an inert diluent such as a suitably purified paraffinic hydrocarbon
  • polymerisation is effected in the gaseous phase, it may be effected by introducing the monomer, for example propylene, into the polymerisation vessel as a liquid and operating with conditions of temperature and pressure within the polymerisation vessel which are such that the liquid monomer vaporises, thereby giving an evaporative cooling effect, and essentially all of the polymerisation occurs with the monomer in the gaseous phase.
  • Polymerisation in the gas phase is preferably effected using conditions which are such that the monomer is at a temperature and partial pressure which are close to the dew point temperature and pressure for that monomer. Such a procedure is described in more detail in published German Patent Application 2 616 356.
  • Polymerisation in the gaseous phase can be effected using any technique suitable for effecting a gas solid reaction such as a fluidised bed reactor system, a stirred bed reactor system or a ribbon blender type of reactor.
  • Polymerisation may be effected either in a batch manner or on a continuous basis and the catalyst components may be introduced into the polymerisation vessel separately or all the catalyst components may be mixed together before being introduced into the polymerisation reactor.
  • the polymerisation can be effected in the presence of a chain transfer agent such as hydrogen or a zinc dialkyl, in order to control the molecular weight of the product formed.
  • a chain transfer agent such as hydrogen or a zinc dialkyl
  • hydrogen is used as the chain transfer agent, it is conveniently used in an amount of from 0.01 up to 5.0%, particularly from 0.05 up to 2.0% molar relative to the monomer.
  • the amount of chain transfer agent will be dependent on the polymerisation conditions, especially the temperature, which is typically in the range from 20°C up to 100°C, preferably from 50°C up to 85°C.
  • propylene may be polymerised to give a polymer having a high flexural modulus, for example at least 1.00 GN/m 2 , particularly at least 1.30 GN/m 2 and especially up to 1.70 GN/ M 2 .
  • Particularly useful copolymers can be obtained using catalysts in accordance with the present invention.
  • a copolymer of propylene and ethylene comprising a sequence of homopolymerised propylene and a sequence of propylene copolymerised with ethylene, said copolymer having a low temperature brittle point of -20°C or lower and a flexural modulus of at least 1.35 GN/m 2 .
  • the flexural modulus is determined in the manner as set out in Note (h) to Table 5 hereafter and the low temperature brittle point is determined in the manner set out in Note (k) to Table 6 hereafter.
  • the flexural modulus may be as high as 1.50 GN/m 2 and preferred copolymers in accordance with the present invention have a flexural modulus of at least 1.40 GN/m 2 .
  • the low temperature brittle point may be as low as -35°C and is preferably -25°C or lower.
  • Particularly preferred copolymers have a low temperature brittle point of -25°C or lower and a flexural modulus of at least 1.40 GN/m 2 .
  • a copolymer of propylene and ethylene comprising a sequence of homopolymerised propylene and a sequence of propylene copolymerised with ethylene, said copolymer having a low temperature brittle point of -40°C or lower and a flexural modulus of at least 1.20 GN/m 2 .
  • the low tempterature brittle point of such copolymers is typically in the range -40°C to -50°C and the flexural modulus may be as high as 1.30 GN/m 2 .
  • Polymers produced by the process of the present invention have a high molecular weight as indicated by the melt flow index measured according to ASTM Test Method D 1238-70, using Condition N (that is a temperature of 190°C and a weight of 10 kgm).
  • Polymers obtained in accordance with the present invention have a melt flow index of less than 200 and preferred polymers have a melt flow index of less than 100, particularly less than 50, for example between 5 and 50.
  • a solution of 4.21 moles of titanium tetrachloride in 2.2 litres of pure n-heptane was placed in a five litre nitrogen-purged dry jacketed glass reaction vessel. The solution was cooled to a temperature in the range 8°C to 10°C and stirred at 250 rpm.
  • a solution of ethyl aluminium sesquichloride in n-heptane (containing 500 grammes of the sesquichloride for each litre of n-heptane) was added to the contents of the reaction vessel over a period of 90 minutes. The quantity added was sufficient to provide 2.868 moles of the ethyl aluminium sesquichloride (this contained 2.868 moles of diethyl aluminium chloride).
  • the temperature was maintained at 8°C to 10°C throughout the addition and the mixture was stirred. At the end of the addition of the sesquichloride solution, the mixture was stirred for a further 4 hours whilst maintaining the temperature of 8°C to 10
  • the whole mixture was then heated up to a temperature of 90°C whilst still stirring.
  • the temperature was maintained at 90°C for 90 minutes, the mixture was allowed to cool and settle, the supernatant liquid was decanted off and the residual solid was then washed 5 times using 2 litres of purified n-heptane for each wash.
  • the washed product was then suspended in 2.5 litres of heptane and the suspension obtained was then split up into several portions.
  • a portion equivalent to one fifth of the suspension obtained by the foregoing procedure was then treated with neat di-n-butyl ether in the following manner.
  • a sufficient quantity of the di-n-butyl ether was added to provide 1.1 mole of the ether for each mole of titanium trichloride present in the suspension, which was being stirred.
  • the addition was effected at room temperature and the product was then heated up to 90°C which temperature was maintained for one hour.
  • tri-n-butyl phosphine was added (neat) in a quantity sufficient to provide 0.084 mole of tri-n-butyl phosphine for each mole or titanium trichloride present.
  • the temperature of 90°C was maintained for a further one hour with stirring.
  • the mixture was then allowed to cool to room temperature and the solid was allowed to settle.
  • the supernatant liquid was decanted off and the solid was then washed 5 times with n-heptane using 500 ml of n-heptane for each wash.
  • a sample of the product was dried and subjected to surface area measurements and to analysis. The remainder of the product was suspended in 500 ml of n-heptane.
  • Example 2 The heat treatment in the presence of di-n-butyl ether described in Example 1 was repeated except that the reaction mixture was maintained at 90°C for a time of 2 hours. This heated product was then allowed to cool and was washed 5 times with n-heptane and finally resuspended in n-heptane. The washing procedure was also as described in Example 1.
  • n-heptane supplied by British Drug Houses and conforming to the Institute of Petroleum specification was passed, at room temperature, through a column containing BTS catalyst and a molecular sieve. After this treatment, the only impurity which could be detected was toluene at a level of about 0.01% by volume. This will be referred to as "purified n-heptane"'.
  • n-heptane A further quantity of n-heptane was purged with nitrogen at ambient temperature for one hour. This will be referred to as "purged n-heptane".
  • the reduction stage was as described in Example 1A) and used the purified n-heptane.
  • the treatment with di-n-butyl ether was effected on a one sixth portion of the product from stage A), the ether being added in an amount of 1.1 moles of ether for each mole of titanium trichloride present and the addition being made when the suspension had attained a temperature of 90°C.
  • 0.084 mole of tri-n-butyl phosphine was added for each mole of titanium trichloride present in the product from stage A), and heating at 90°C was continued for a further hour.
  • the product obtained was allowed to cool and was washed as in Example 1. All stages of the preparation, other than the last three washes, were effected using purified n-heptane. The last three- washes were effected using purged n-heptane and the product was suspended in purged n-heptane.
  • Example 1 During this preparation the suspension could be handled easily and there were no problems of agglomeration of the solid particles. In the process of Example 1 there were agglomeration problems and these problems were reduced only when the temperature of 90°C was attained.
  • the product of this Example had a superior particle form compared to the product of Example 1, and could be handled more readily than the product of Example 1.
  • Example 2 The procedure of Example 2 was repeated except that the quantity of tri-n-butyl phosphine was 0.028 mole for each mole of titanium trichloride.
  • Example 2 The procedure of Example 2 was repeated except that the quantity of tri-n-butyl phosphine was 0.14 mole for each mole of titanium trichloride.
  • Example 2 The procedure of Example 2 was repeated except that the treatment with di-n-butyl ether, and the subsequent addition of tri-n-butyl phosphine, were effected at temperatures other than 90°C. Additionally subsequent to the heating of the reduction product all the washing and heating steps were effected in a mixed aliphatic hydrocarbon consisting predominantly of C 12 isomers.
  • the reduced and heat-treated solid used in the preparation of the products of Examples 5 to 7 was heated to 90°C and 1.1 moles of di-n-butyl ether was added for each mole of titanium trichloride and the temperature maintained at 90°C for two hours and the product obtained was washed 5 times. Subsequent to the heating of the reduction product, all stages were effected using the same aliphatic hydrocarbon as was used in Examples 5 to 7.
  • Example 2 The procedure of Example 2 was repeated except that di-n-butyl ether and tri-n-butyl phosphine were mixed together and the mixture formed was added to the reduction product when it attained a temperature of 90°C. The temperature of 90°C was maintained for two hours.
  • Example 2 The procedure of Example 2 was repeated except that the tri-n-butyl phosphine was added first, when the temperature attained 90°C, and the di-n-butyl ether was added after the mixture had been at 90°C for one hour.
  • Example 2 The procedure of Example 2 was repeated except that only di-n-butyl ether was added to the reduction product at 90°C, the temperature was maintained for two hours, the mixture was allowed to cool to ambient temperature (about 20°C), and then the tri-n-butyl phosphine was added. The solid was contacted with the tri-n-butyl phosphine at ambient temperature for 30 minutes and was then washed as in Example 2.
  • Example 2 The procedure of Example 2 was repeated except that the thermal treatment of the reduced solid was either omitted or varied. Details of the thermal treatment are set out in Table 2.
  • Example 2 The procedure of Example 2 was repeated except that different proportions of di-n-butyl ether were used, as set out in Table 3.
  • titanium trichioride prepared as described in Examples 1 to 15 or Comparative Examples A or B
  • 0.134 mole of titanium trichioride was added as a suspension of titanium trichloride in the hydrocarbon diluent. 2 litres of the hydrocarbon diluent were then added.
  • the autoclave was maintained at 60°C while propylene was passed into the autoclave at a constant rate of 22 pounds per hour (about 10 kilograms per hour).
  • the propylene charge contained 0.15% by volume of hydrogen.
  • a total of 33.5 kilograms of propylene were passed into the autoclave, after which the propylene feed was terminated and the autoclave pressure was allowed to run down to 5 psi (34.5 kN/m 2 ) gauge.
  • the residual propylene was then vented off and the polymer suspension passed into a glass-lined vessel.
  • the autoclave was washed with 20 litres of the diluent which was also added to the glass-lined vessel.
  • the contents of the glass-lined vessel were mixed with isopropanol in an amount of 2% by volume relative to the diluent.
  • the mixture was stirred for 1 hour at 70°C, a mixture of isopropanol and water (containing 10% by volume of water) was added in an amount of 0.6% by volume relative to the diluent and stirring at 70°C was continued for a further 2 hours.
  • the polymer suspension was then run into a further vessel containing 40 litres of demineralised water at ambient temperature, and the mixture was stirred for 30 minutes.
  • the aqueous phase was then decanted off and a further 40 litres of demineralised water at ambient temperature were added and the process was repeated.
  • the diluent was then filtered off and the polymer was dried at 100°C in the fluidised bed using nitrogen as fluidising gas.
  • Example 2 The product of Example 2 was used to prepare a copolymer of propylene with ethylene.
  • Polymerisation was effected in a 20 gallon (91 litre) stainless steel autoclave.
  • 64 litres of the hydrocarbon diluent (as used in Examples 16 to 30) were charged into the vessel and degassed at 60°C for 30 minutes at a pressure of 50 mm Hg.
  • Propylene containing 0.145% by volume of hydrogen was then admitted to the vessel at a rate of 221bs/hour in an amount to give a pressure of 1 psi (6.9 kN/m 2 ) gauge.
  • a vent on the vessel was opened and the propylene/hydrogen addition was continued for a further 5 minutes, the pressure in the autoclave being maintained at 1 psi (6.9 kN/m 2 ) gauge throughout.
  • the autoclave temperature was maintained at 60°C whilst a total of 55.3 Ibs (25.1 kg) of propylene containing 0.145% by volume of hydrogen was passed into the autoclave at a constant rate of 22 Ibs/hour (about 10 kg/hour), after which the propylene/hydrogen feed was terminated and the autoclave pressure was allowed to run down to 18 psi (124 kN/m 2 ) gauge, (equivalent to 30 psi (207 kN/m 2 ) absolute of propylene), the excess pressure being due to the presence of inert materials.
  • a total of 4.4 kg of ethylene was then metered into the autoclave at a feed rate of 2.3 kg/hour for 20 minutes, then 4.0 kgm/hcur for 56 minutes.
  • the ethylene feed was then terminated and the autoclave pressure allowed to run down to a total pressure of 2 psi (13.8 kN/m 2 ) gauge.
  • the polymer suspension was passed into a 20 gallon (91 litre) glass-lined vessel.
  • the autoclave was washed with 20 litres of the hydrocarbon diluent which was also added to the glass-lined vessel.
  • the contents of the glass-lined vessel were mixed with isopropanol in an amount of 3% by volume relative to the diluent.
  • the mixture was stirred for t hour at 70°C, and a mixture of isopropanol and distilled water (containing 10% by volume of water) was added in an amount of 0.6% by volume relative to the diluent and stirring at 70°C continued for a further 1 t hours.
  • the polymer suspension was run into a further 20 gallon vessel containing 40 litres of demineralised water at ambient temperature and the mixture was stirred for 30 minutes. The stirrer was then stopped and the aqueous phase decanted off. A further 40 litres of demineralised water was added, stirring restarted and the process repeated. The diluent was then filtered off and the polymer was dried at 100°C in a fluidised bed using nitrogen as the fluidising gas.
  • the polymer obtained had the properties set out in Table 6.
  • Example 2 The procedure of Example 2 was repeated with the exception that the n-heptane was replaced by a hydrocarbon fraction consisting mainly of e 7 isomers and having a boiling point range of 97°C to 103°C (this material will hereafter be referred to as "diluent 7").
  • Titanium tetrachloride was reduced with ethyl aluminium sesquichloride using the procedure of Example 1 with the exception that the n-heptane was replaced by diluent 7. At the end of the addition of the sesquichloride solution, the mixture was stirred for a further 4 hours whilst maintaining a temperature of 8°C to 10°C.
  • a sample containing about one mole of titanium trichloride was separated from the reaction mixture and the suspension was diluted by the addition of an equal volume of a mixed aliphatic hydrocarbon fraction consisting predominantly of e 12 isomers.
  • the mixture was then heated at 102°C and maintained at that temperature for 90 minutes.
  • the supernatant liquid was decanted off and the solid was then washed five times with 700 ml of the mixed aliphatic hydrocarbon fraction.
  • the washed product was then suspended in 700 ml of the aliphatic hydrocarbon fraction.
  • the product was then created with di-n-butyl ether and tri-n-butyl phosphine as described in Example 2 with the exception that the mixed aliphatic hydrocarbon fraction was used for all stages except the final washes which were effected using diluent 7, the temperature used was 110°C and 0.112 mole of tri-n-butyl phosphine was used.
  • the final product was suspended in 700 ml of the mixed aliphatic hydrocarbon fraction.
  • Example 2 The procedure of Example 2 was repeated with a number of variations as follows:
  • Reduction was effected by adding a 25% by weight solution of diethyl aluminium chloride, in an amount sufficient to provide 2.8 moles of the diethyl aluminium chloride, to 4 moles of titanium tetrachloride.
  • the reduced product was initially heated at 110°C.
  • the product obtained was finally suspended in the mixed aliphatic hydrocarbon fraction to give a titanium trichloride concentration of 0.9 mole per litre of suspension.
  • Example 2 The procedure of Example 2 was repeated with the exception that the n-heptane was replaced by the mixed aliphatic hydrocarbon fraction, the reduced and heated product was split into three portions for the treatment with the ether and phosphine, variations in this latter treatment being indicated in Table 7.
  • a solution of 4.00 moles of titanium tetrachloride in 880 ml of the mixed aliphatic hydrocarbon fraction was placed in a 6.5 litre nitrogen-purged dry jacketed glass reaction vessel. The solution was maintained at a temperature of 25°C and stirred at 250 rpm.
  • a solution of ethyl aluminium sesquichloride in the mixed aliphatic hydrocarbon fraction (containing 0.85 mole of diethyl aluminium chloride for each litre of the solution) was added to the contents of the reaction vessel over a period of 4 hours. The quantity added was sufficient to provide 2.0 moles of the ethyl aluminium sesquichloride (this contained 2.0 moles of diethyl aluminium chloride).
  • the temperature was maintained at 25°C throughout the addition and the mixture was stirred. At the end of the addition of the sesquichloride solution, the mixture was stirred for a further one hour whilst maintaining the temperature of 25°C.
  • the whole mixture was then heated up to a temperature of 90°C whilst still stirring.
  • the temperature was , maintained at 90°C for 90 minutes, the mixture was allowed to cool and settle, the supernatant liquid was decanted off and the residual solid was then washed five times using 3 litres of the mixed aliphatic hydrocarbon fraction for each wash.
  • the washed product was then suspended in 3 litres of the mixed aliphatic hydrocarbon fraction and the suspension obtained was then split up into several portions.
  • Example 34 The procedure of Example 34 was repeated with the exception that the conditions of treatment with di-n-butyl ether and tri-n-butyl phosphine were varied. The changes are summarised in Table 9.
  • Example 34 The procedure of Example 34 was repeated with the exception that the treatment with di-n-butyl ether and tri-n-butyl phosphine was effected at 115°C and 0.10 mole of tri-n-butyl phosphine was used.
  • a solution of 4.00 moles of titanium tet:achloride in 880 ml of the mixed aliphatic hydrocarbon fraction was placed in a 6.5 litre nitrogen-purged dry jacketed glass reaction vessel. The solution was cooled to a temperature of 0°C and stirred at 250 rpm. A 25% by weight solution of diethyl aluminium choride in the mixed aliphatic hydrocarbon fraction was added to the contents of the reaction vessel over a period of 8 hours. The quantity added was sufficient to provide 2.8 moles of the diethyl aluminium chloride. The temperature was maintained at 0°C throughout the addition and the mixture was stirred. At the end of the addition of the diethyl aluminium chloride solution, the mixture was stirred for a further 2 hours whilst maintaining the temperature of 0°C.
  • the whole mixture was then heated up to a temperature of 100°C whilst still stirring. The temperature was maintained at 100°C for 90 minutes, the mixture was allowed to cool and settle, the supernatant liquid was decanted off and the residual solid was then washed twice using 3 litres of the mixed aliphatic hydrocarbon fraction for each wash. The washed product was then suspended in 3 litres of the mixed aliphatic hydrocarbon fraction and a one-sixth portion was separated.
  • the one-sixth portion separated in A) was treated with di-n-butyl ether and tri-n-butyl phosphine in the manner described in Example 2 except that n-heptane was replaced by the mixed aliphatic hydrocarbon fraction, the temperature used was 120°C and 0.10 mole of tri-n-butyl phosphine was used.
  • the residual major portion from A) was heated, with stirring, to 100°C.
  • di-n-butyl ether was added in an amount of 1.1 moles of ether for each mole of titanium trichloride present and the mixture was stirred at 100°C for one hour and was then separated into two portions equal to one-half and one-third of the washed product of A).
  • One of the portions from C) was washed twice more with 500 ml of the mixed aliphatic hydrocarbon fraction and finally suspended in 500 ml of the mixed aliphatic hydrocarbon fraction.
  • the one-half portion from B) was washed twice with 1.5 litres of the mixed aliphatic hydrocarbon fraction and suspended in 1.5 litres of the mixed aliphatic hydrocarbon fraction. A one-third portion was then separated.
  • the one-third portion from D) was heated, with stirring, to 100°C, 0.10 mole of tri-n-butyl phosphine for each mole of titanium trichloride, was added on attaining 100°C, and the temperature of the mixture was maintained at 100°C for one hour. The mixture was then allowed to settle and cool, washed four times with 500 ml of the mixed aliphatic hydrocarbon fraction and finally suspended in 500 ml of the mixed aliphatic hydrocarbon fraction.
  • the residual portion from D) was heated, with stirring, to 100°C, 1.1 moles of di-n-butyl ether, for each mole of titanium trichloride, were added on attaining 100°C and the temperature was maintained at 100°C for one hour.
  • Example 50 The procedure of Example 50 was repeated with the exception that the initial heating was up to a temperature of 100°C, the treatment with the ether and the phosphine was effected at 115°C and the final product was washed five times.
  • Polymerisation was effected in a 20 gallon (91 I) stainless steel autoclave.
  • 64 litres of the hydrocarbon diluent (as used in Examples 16 to 30) were charged into the vessel and degassed at 60°C for 30 minutes at a pressure of 50 mm Hg.
  • Propylene containing 0.175% by volume of hydrogen was then admitted to the vessel at a rate of 22 lbs/hr in an amount to give a pressure of 1 psi (6.9 kN/m 2 ) gauge.
  • a vent on the vessel was opened and the proylene/hydrogen addition was continued for a further 5 minutes, the pressure in the autoclave being maintained at 1 psi (6.9 kN/m 2 ) gauge throughout.
  • the autoclave temperature was maintained at 60°C whilst a total of 60.3 Ibs (27.4 kg) of propylene containing 0.175 volume % of hydrogen was passed into the autoclave at a constant rate of 22 Ibs/hour (about 10 kg/hour), after which the propylene/hydrogen feed was terminated and the autoclave pressure was allowed to run down to 10 psi (69 kN/m 2 ) gauge, (equivalent to 20 psi (138 kN/m2) absolute) of propylene, the excess pressure being due to the presence of inert materials.
  • a total of 2.07 kg of ethylene was then metered into the autoclave at a feed rate of 2.3 kg/hour for 20 minutes, then 4.0 kgm/hour for 20 minutes.
  • the ethylene feed was then terminated and the autoclave pressure allowed to run down to a total pressure of 2 psi (13.8 kN/m 2 ) gauge.
  • the polymer suspension was passed into a 20 gallon (91 I) glass-lined vessel.
  • the autoclave was washed with 20 litres of the hydrocarbon diluent which was also added to the glass-lined vessel.
  • the contents of the glass-lined vessel were mixed with isopropanol in an amount of 3% by volume relative to the diluent.
  • the mixture was stirred for 2 hour at 70°C, and a mixture of isopropanol and distilled water (containing 10% by volume of water) was added in an amount of 0.6% by volume relative to the diluent and stirring at 70'C continued for a further 11 ⁇ 2 hours.
  • the polymer suspension was run into a further 20 gallon vessel containing 40 litres of demineralised water at ambient temperature and the mixture was stirred for 30 minutes. The stirrer was then stopped and the aqueous phase decanted off. A further 40 litres of demineralised water were added, stirring restarted and the process repeated. The diluent was then filtered off and the polymer was dried at 100°C in a fluidised bed using nitrogen as the fluidising gas.
  • a homopolymerisation process was carried out continuously in a series of 5 interconnected 5 gallon (22.7 litres) stainless steel autoclaves wherein the transfer lines between each adjacent pair of vessels were provided with isolation valves.
  • each of the second, third, fourth and fifth autoclaves was placed a sample of a live polymer suspension (that is one in which there had been no treatment to deactivate the catalyst) which had been prepared by a technique as described in Examples 16 to 30 but omitting the treatment with isopropanol, and subsequent treatments.
  • the contents of these vessels were stirred, the vessels were maintained at 60°C and the isolation valves were kept closed.
  • a separate homopolymerisation was effected in the first vessel at 60°C by adding propylene gas containing 0.26% by volume of hydrogen, at a rate sufficient to maintain the autoclave pressure at 35 psi (241 kN/m 2 ) gauge into 15 litres of stirred, degassed hydrocarbon diluent containing 0.14 mole diethyl aluminium chloride and 0.07 mole of the titanium trichloride product of Example 41.
  • Second vessel - The propylene/hydrogen mixture was also added to this vessel.
  • the relative rates of feed of the propylene/hydrogen mixture to the first and second vessels were controlled in dependence on the liquid level of the suspension in each vessel to maintain the levels in each vessel at between 22 and 25 litres of suspension.
  • the suspension of homopolymer formed in the fifth vessel was passed from this vessel into a continuous cascade deashing system, which provided a similar treatment to that described in Examples 16 to 30.
  • the rate of removal of the homopolymer suspension from the fifth vessel was controlled to maintain equilibrium levels within the system.
  • Homopolymerisation was effected continuously for 30 hours.
  • a copolymerisation process was carried out continuously in the apparatus described in Example 81.
  • each of the second, third, fourth and fifth autoclaves was placed a sample of a live polymer suspension (that is one in which there had been no treatment to deactivate the catalyst) which had been prepared by a technique as described in Examples 16 to 30 but omitting the treatment with isopropanol, and subsequent treatments.
  • the contents of these vessels were stirred, the vessels were maintained at 60°C and the isolation valves were kept closed.
  • a separate homopolymerisation was effected in the first vessel at 60°C by adding propylene gas containing 0.32% by volume of hydrogen, at a rate sufficient to maintain the autoclave pressure at 35 psi (241 kN/m 2 ) gauge into 15 litres of stirred, degassed hydrocarbon diluent containing 0.12 mole diethyl aluminium chloride and 0.06 mole of the titanium trichloride product of Example 41.
  • Second vessel - The propylene/hydrogen mixture was also added to this vessel.
  • the rotative rates of feed of the propylene/hydrogen mixture to the first and second vessels were controlled in dependence on the liquid level of the suspension in each vessel to maintain the levels in each vessel at between 22 and 25 litres of suspension.
  • the suspension of copolymer formed in the fifth vessel was passed from this vessel into a continuous cascade deashing system, which provided a similar treatment to that described in Examples 16 to 30.
  • the rate of removal of the copolymer suspension from the fifth vessel was controlled to maintain equilibrium levels within the system.
  • Titanium tetrachloride was reduced, heated to 100°C, cooled, washed and finally resuspended as described in stage A) of Examples 45 to 49.
  • Examples 83 to 85 The procedure of Examples 83 to 85 was repeated with the exception that the titanium tetrachloride solution was more dilute (1 volume of titanium tetrachloride to 4 volumes of the mixed aliphatic hydrocarbon fraction), the temperature was 110°C, and 0.10 mole, for each mole of titanium trichloride, of triphenyl phosphine oxide was used.
  • Examples 97 to 99 The procedure of Examples 97 to 99 was repeated with the exception that the ether was diphenyl ether (used as a mixture of 75% by weight of diphenyl ether and 25% by weight of diphenyl) and the phosphorus compound used was tri-n-butyl phosphine.
  • the ether was diphenyl ether (used as a mixture of 75% by weight of diphenyl ether and 25% by weight of diphenyl) and the phosphorus compound used was tri-n-butyl phosphine.
  • Example 2 The samples were each divided into a number of portions which were treated as generally described in Example 2 with the exception that the temperature was varied, different phosphorus compounds were used in varying proportions, the mixed aliphatic hydrocarbon fraction was used throughout (rather than n-heptane), and the heated product was washed only three times. Further details are set out in Table 17.
  • Titanium tetrachloride was reduced using the procedure described in stage A) of Examples 45 to 49.

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Claims (17)

1. Composition caractérisée par la formule:
Figure imgb0031
et ayant un spectre de diffraction des rayons X qui est soit celui de la forme bête du trichlorure de titane, soit celui de la forme bêta du trichlorure de titane qui renferme également des raies caractéristiques des formes de réseaux en couches du trichlorure de titane; ou
R est un groupe hydrocarbyle;
X est un atome d'halogène autre que le fluor;
E est un éther ou un thioéther qui contient seulement au moins un groupe éther ou seulement au moins un groupe thioéther;
L est un composé organique formant Base de Lewis contenant du phosphore;
x est tel que 0<x<3,0;
n est compris entre 0 et 0,5; et
a et b sont chacun, indépendamment, compris entre 0,001 et 0,50.
2. Composition suivant la revendication 1, caractérisée en ce que le groupe R est un groupe alcoyle contenant de 2 à 10 atomes de carbone et X est du chlore, et la valeur de x est telle que OGx<2,0.
3. Composition suivant la revendication 1 ou 2, caractérisée en ce que E est de l'éther di-n-butylique, de l'éther di-isoamylique ou de l'éther diphénylique.
4. Composition suivant l'une quelconque des revendications 1 à 3, caractérisée en ce que le composé L est un composé de formule générale
Figure imgb0032
où
R3 est un groupe hydrocarbyle ou un groupe hydrocarbyloxy où le groupe hydrocarbyle contient jusqu'à 18 atomes de carbone;
R4 et R5, qui peuvent être identiques ou différents, sont chacun un atome d'hydrogène ou un groupe R3; et
m est 0 ou 1.
5. Composition suivant la revendication 4, caractérisée en ce que le composé L est de la tri-n-butyl-phosphine, de la triphényl-phosphine, de l'oxyde de tri-n-butyl-phosphine, de l'oxyde de trioctvl- phosphine, de l'oxyde de triphényl-phosphine, du phosphite tri-n-butylique, du phosphite triphénylique, du phosphite tris(nonylphénylique), du phosphate triéthylique, du phosphate tri-n-butylique ou du phosphate triphénylique.
6. Composition suivant l'une quelconque des revendications 1 à 5, caractérisée en ce que les valeurs de a et b sont différentes, la valeur de a allant de 0,01 à 0,20 et la valeur de b allant de 0,005 à 0,20.
7. Composition suivant l'une quelconque des revendications 1 à 6, caractérisée en ce que la surface spécifique est comprise entre 1 et 30 m2/g.
8. Procédé pour la production d'une composition contenant du trichlorure de titane, consistant
1) à réduire du tétrachlorure de titane par réaction du tétrachlorure de titane avec un agent réducteur dans des conditions donnant un produit contenant du trichlorure de titane qui renferme un composé d'aluminium associé contenant des atomes d'aluminium et de chlore, dans lequel le trichlorure de titane est formé de façon prédominante sous la forme bêta;
2) à amener le produit de la réduction en contact avec un composé organique formant Base de Lewis L; et
3) à laver avec un liquide constitué par un hydrocarbure inerte ou un hydrocarbure halogéné inerte; caractérisé en ce qu'au cours du stade 2) le produit de la réduction est amené en contact, simultanément ou successivement, avec le composé E et avec le composé L, au moins une partie de la mise en contact étant effectuée à une température d'au moins 60°C, en présence au moins du composé E ou du composé L, et en ce que le lavage est effectué ultérieurement à la mise en contact avec le composé E, où E est un éther ou un thioéther qui contient seulement au moins un groupe éther ou seulement au moins un groupe thioéther; et L est un composé organique formant Base de Lewis contenant du phosphore.
9. Procédé suivant la revendication 8, caractérisé en ce que le produit du stade 1 ) est soumis à un traitement thermique à une température comprise dans une gamme allant de 40°C à 130°C pendant une période de temps allant de cinq minutes à vingt heures et en ce que le produit ayant subi le traitement thermique est ensuite soumis au stade 2) du processus.
10. Procédé suivant la revendication 8 ou 9, caractérisé en ce que l'agent réducteur est un composé organique d'aluminium de formule
Figure imgb0033
et en ce que la réduction est effectuée sensiblement en l'absence d'hydrocarbures aromatiques, où R est un groupe hydrocarbyle; X est un atome d'halogène autre que le fluor; et x' est tel que 1.0≤x'≤3,0.
11. Procédé suivant l'une quelconque des revendications 8 à 10, caractérisé en ce qu'au cours du stade 2) le composé E et le composé L sont ajoutés séparément, le composé E étant ajouté le premier et l'addition étant effectuée dès que le produit de la réduction atteint la température d'au moins 60°C.
12. Procédé suivant l'une quelconque des revendications 8 à 11, caractérisé en ce qu'au cours du stade 2) le produit de la réduction est amené en contact avec le composé E à la température d'au moins 60°C, le produit est lavé et le produit lavé est amené en contact avec le composé L à la température d'au moins 60°C.
13. Procédé suivant l'une quelconque des revendications 8 à 12, caractérisé en ce qu'au cours du stage 2) le produit de la réduction est chauffé à une température comprise entre 90°C et 120°C et en ce que le temps de chauffage est d'au moins deux heures et n'est pas supérieur à dix heures.
14. Catalyseur de polymérisation des oléfines comprenant:
1 ) un matière contenant du trichlorure de titane; et
2) au moins un composé organo-métallique d'aluminium ou d'un métal autre qu'un métal de transition du groupe IIA de la classification périodique, ou un complexe d'un composé organo-métallique d'un métal autre qu'un métal de transition du groupe IA ou du groupe IIA de la classification périodique avec un composé organique d'aluminium,

caractérisé en ce que le constituant 1) est une composition suivant l'une quelconque des revendications 1 à 7 ou est un produit obtenu par le procédé suivant l'une quelconque des revendications 8 à 13.
15. Procédé pour la production d'un polymère ou d'un copolymère d'un monomère oléfinique suivant lequel au moins un monomère oléfinique est polymérisée par mise en contact d'au moins cette oléfine, dans des conditions de polymérisation, avec un catalyseur de polymérisation des oléfines, caractérisé en ce que le catalyseur de polymérisation des oléfines est un catalyseur suivant la revendication 14.
16. Copolymère de propylène et d'éthylène obtenu par le procédé suivant le revendication 15 et comprenant une séquence de propylène homopolymérisé et une séquence de propylène copolymérisé avec de l'éthylène, ce copolymère ayant un point de fragilisation à basse température de -25°C ou inférieur et un module de flexion d'au moins 1,40 GN/m2.
17. Copolymère de propylène et d'éthylène obtenu par le procédé suivant la revendication 15 et comprenant une séquence de propylène homopolymérisé et une séquence de propylène copolymérisé avec de l'éthylène, ce copolymère ayant un point de fragilisation à basse température de -40°C ou inférieur et un module de flexion d'au moins 1,20 GN/m2.
EP78300283A 1977-08-31 1978-08-14 Compositions à base de trichlorure de titane, préparation de celles-ci, système catalytique les contenant et polymérisation des oléfines à l'aide de ce système Expired EP0000997B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
GB3634177 1977-08-31
GB3634177 1977-08-31
GB2173278 1978-05-24
GB2173278 1978-05-24

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EP0000997A1 EP0000997A1 (fr) 1979-03-07
EP0000997B1 true EP0000997B1 (fr) 1981-11-25

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US (1) US4340502A (fr)
EP (1) EP0000997B1 (fr)
JP (1) JPS5446189A (fr)
AU (1) AU3924078A (fr)
BR (1) BR7805645A (fr)
CA (1) CA1139497A (fr)
DE (1) DE2861357D1 (fr)
ES (1) ES472991A1 (fr)
NO (1) NO782807L (fr)
NZ (1) NZ188206A (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4211670A (en) * 1979-01-25 1980-07-08 Hercules Incorporated Titanium trichloride catalyst component for propylene polymerization
FR2593087B1 (fr) * 1986-01-20 1990-09-07 Bp Chimie Sa Elutriation par un liquide de catalyseurs solides de polymerisation des olefines.

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1391068A (en) * 1971-03-23 1975-04-16 Solvay Preparation of a catalytic complex for use in the poly merisation of alpha-olefins
BE822941A (fr) * 1973-12-04 1975-06-04 Polymeres d'olefines
BE831886A (fr) * 1974-07-31 1975-11-17 Procede de fabrication de trichlorure de titane solide, ce catalyseur et son emploi en tant que catalyseur pour la polymerisation d'alpha-olefines
US3984350A (en) * 1974-05-09 1976-10-05 Standard Oil Company (Indiana) Catalyst component comprising brown titanium trichloride
JPS5291794A (en) * 1976-01-30 1977-08-02 Mitsubishi Chem Ind Ltd Preparation of alpha-olefin polymerization catalyst

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL269009A (fr) * 1960-09-07
US3186977A (en) * 1961-03-01 1965-06-01 Eastman Kodak Co Three-component alkyl aluminum catalysts for olefin polymerization
NO139131C (no) 1969-10-20 1979-01-10 Mitsui Petrochemical Ind Fremgangsmaate ved fremstilling av en katalysatorblanding for anvendelse ved polymerisering av olefiner.
FR2099150A5 (fr) * 1970-06-18 1972-03-10 Mitsui Toatsu Chemicals
JPS4932195B1 (fr) 1970-10-02 1974-08-28
JPS4933957B1 (fr) * 1970-12-25 1974-09-11
JPS4834281A (fr) 1971-09-04 1973-05-17
JPS5236877B2 (fr) 1973-11-02 1977-09-19
GB1479651A (en) 1974-01-31 1977-07-13 Ici Ltd Olefine polymerisation catalyst
GB1487393A (en) 1974-02-12 1977-09-28 Ici Ltd Process for the preparation of a titanium trihalide catalyst component
DE2413261A1 (de) * 1974-03-20 1975-09-25 Hoechst Ag Verfahren zur herstellung eines katalysators
GB1503305A (en) 1974-07-11 1978-03-08 Isr Holding Sarl Preparation and use of a ziegler catalyst
US3992320A (en) * 1974-08-24 1976-11-16 Basf Aktiengesellschaft Manufacture of a modified titanium component for catalysts of the Ziegler-Natta type
AU502749B2 (en) * 1975-06-16 1979-08-09 Imperial Chemical Industries Limited Production of transition metal composition
JPS527891A (en) * 1975-07-09 1977-01-21 Toa Nenryo Kogyo Kk Process for producing catalyst components for polymerization of olefi n
JPS527892A (en) 1975-07-09 1977-01-21 Toa Nenryo Kogyo Kk Process for producing catalyst components for polymerization of alpha-olefin
IT1040379B (it) * 1975-08-08 1979-12-20 Montedison Spa Componenti catalitici e catalizzatori per la polimerizzazione delle olefine
FR2340131A1 (fr) * 1976-02-03 1977-09-02 Naphtachimie Sa Procede de fabrication de catalyseurs pour la polymerisation des olefines
DE2616260A1 (de) 1976-04-13 1977-11-03 Basf Ag Verfahren zur herstellung von poly-alpha-olefinen
US4111836A (en) * 1976-11-03 1978-09-05 Standard Oil Company (Indiana) Process for forming high performance titanium trichloride olefin polymerization catalyst components

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1391068A (en) * 1971-03-23 1975-04-16 Solvay Preparation of a catalytic complex for use in the poly merisation of alpha-olefins
BE822941A (fr) * 1973-12-04 1975-06-04 Polymeres d'olefines
US3984350A (en) * 1974-05-09 1976-10-05 Standard Oil Company (Indiana) Catalyst component comprising brown titanium trichloride
BE831886A (fr) * 1974-07-31 1975-11-17 Procede de fabrication de trichlorure de titane solide, ce catalyseur et son emploi en tant que catalyseur pour la polymerisation d'alpha-olefines
JPS5291794A (en) * 1976-01-30 1977-08-02 Mitsubishi Chem Ind Ltd Preparation of alpha-olefin polymerization catalyst

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Journal of Catalysis, vol. 8, page 189 *
Macromulecular Reviews volume 2, Interscience Publ. page 125, lignes 10-12 *

Also Published As

Publication number Publication date
CA1139497A (fr) 1983-01-11
BR7805645A (pt) 1979-04-10
AU3924078A (en) 1980-02-28
DE2861357D1 (en) 1982-01-28
US4340502A (en) 1982-07-20
EP0000997A1 (fr) 1979-03-07
ES472991A1 (es) 1979-10-16
NO782807L (no) 1979-03-01
NZ188206A (en) 1980-04-28
JPS5446189A (en) 1979-04-11

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