Classifications

• • 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
  • C08F4/00—Polymerisation catalysts
  • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
  • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
  • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
  • C08F4/62—Refractory metals or compounds thereof
  • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
• • 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

Definitions

• the present invention relates to a process for the preparation of a Ziegler-type catalyst for the polymerization of olefins, the catalyst thus obtained and a process for the polymerization of olefins using it.
• JP-A-53 / 81,492 (1978) describes a solid catalyst for the polymerization of alpha-olefins comprising a titanium-containing solid prepared by a process comprising the liquefaction of an anhydrous magnesium halide in a halogenated hydrocarbon in the presence of aluminum halide, bringing the solution obtained into contact with an initiator to precipitate a solid mass which is then, or simultaneously with its formation, brought into contact with a halogenated titanium compound.
• the aluminum halide can be obtained by reacting a haloalkylaluminum with the chlorinated solvent.
• the initiator can be a halogenated titanium compound, an electron donor or a complex of these products. All the examples provided in this document include the use of an electron donor and, moreover, the published data show that the halogenated titanium compound remains at valence (IV).
• the temperature of use of the catalysts described in this document in polymerization is less than or equal to
• the catalyst used comprises a titanium compound in the liquid state obtained by treating a titanium tetrahalogenide in a hydrocarbon and / or a halogenated hydrocarbon, in the presence of an ether, by means of a compound which may be an organoaluminum compound or an organomagnesium compound, used according to the examples given in a stoichiometric amount relative to the titanium compound.
• the temperature of use of the catalysts described in this document, in copolymerization to obtain amorphous copolymers is less than or equal to 120 ° C.
• the problem posed by the present invention is, in the context of Ziegler catalysts suspended in a dihaloalkane, of obtaining a stable catalyst having good performance, that is to say leading to high yields of polymer, in particular at temperature high
• An object of the present invention consists in a process for the preparation of a catalyst for the polymerization of olefins comprising, in a first step, the reduction of a titanium compound (IV) in an ⁇ , ⁇ -dihaloalkane by means of a molar excess of at least one halogenated organoaluminum compound, in the absence of an ether, characterized in that it comprises, in a second step, the addition to the reaction mixture of a compound capable of forming a magnesium halide in situ, without further reduction of the titanium compound obtained during the first step.
• the titanium compound (IV) to be reduced advantageously has the general formula Ti (OR) n X 4 _ n in which X is a halogen, R is an alkyl radical having from 1 to 10 carbon atoms and 0 ⁇ n ⁇ 4. Titanium tetrachloride TiCl 4 is preferably used.
• a vanadium compound (III), (IV) or (V) can be added to the titanium compound (IV) before, during or after reduction. Its general formula is VX 3 , VX 4 or VO (OR) - m X 3 _ m in which X is a halogen, preferably chlorine, R is an alkyl radical having from 1 to 6 carbon atoms and 0 ⁇ m ⁇ 3.
• the pentavalent vanadium compound contains at least one chlorine atom.
• VOCl 3 oxytrichloride is used for example for addition before reduction, VCl 3 for addition after reduction of the titanium compound (IV).
• the ⁇ , ⁇ -dihaloalkane used as suspension medium for the catalyst according to the invention has the general formula X- (CH 2 ) n -X 'in which X and X', identical or different, are each a halogen atom , such as chlorine, bromine and fluorine and n is an integer between 1 and 10, preferably between 1 and 6.
• X and X' identical or different, are each a halogen atom , such as chlorine, bromine and fluorine and n is an integer between 1 and 10, preferably between 1 and 6.
• the nature of the halogen atoms and the value of n are such that 1' ⁇ , ⁇ - dihaloalkane is liquid under normal conditions of temperature and pressure.
• dichloromethane, 1,2-dichloroethane, 1,4-dichlorobutane and their mixtures are advantageously chosen.
• the halogenated organo-aluminum compound used to reduce the titanium compound (IV) is chosen from: - the compounds of general formula R n AlX 3 _ n in which R is an alkyl radical having from 1 to 4 carbon atoms, X is halogen and 1 ⁇ n ⁇ 2. Examples include dichloroethylaluminium, chlorodiethylaluminium and their mixtures. - the compounds of general formula X 2 A1 (CH 2 ) nAlX2 in which X is a halogen atom and 1 ⁇ n ⁇ 8. They can be obtained by reaction of aluminum with an ⁇ , ⁇ -dihaloalkane.
• Examples include the compounds of formula Cl 2 AlCH 2 AlCl 2 and Cl 2 Al (CH 2 ) 2 AlCl 2 .
• the process according to the invention can be carried out in the presence, in addition, of an inert solvent advantageously chosen from saturated aliphatic or cycloaliphatic hydrocarbons whose boiling point under atmospheric pressure is not less than 60 ° C. It may especially be a saturated aliphatic or cycloaliphatic hydrocarbon having from 6 to 14 carbon atoms, for example a cut of saturated C 10 -C 12 aliphatic hydrocarbons.
• the amount of inert solvent is chosen such that the catalyst obtained is in the form of a suspension which can be handled.
• the method according to the invention can also be implemented in the presence of at least one ⁇ -olefin having at least 4 carbon atoms, in order to promote the activity of the active centers of the catalyst.
• ⁇ -olefin it is advantageous to use methyl-4-pentene-1, hexene-1, octene-1, decene-1, in an amount which can range up to 10 times the molar amount of compound of titanium (IV).
• R and R' identical or different, are alkyl radicals having from 1 to 12 carbon atoms.
• n-butylethylmagnesium or n-butyl-n-octylmagnesium or their mixtures are used.
• the process according to the invention can be carried out in a stirred reactor at a temperature between 0 and 80 ° C. The usual precautions are taken to avoid loss of volatile products by operating under adequate pressure.
• the presence of an ⁇ , ⁇ -dihaloalkane in the reaction medium has the effect of promoting the reduction of the titanium compound (IV) essentially up to a titanium compound (III), whereas if the ⁇ , ⁇ -dihaloalkane is absent, the formation of titanium compound (II) is very important.
• the relative proportions of the various reagents used in the process according to the invention are the following, expressed in molar ratios: ⁇ , ⁇ -dihaloalkane / titanium compound, and optionally vanadium: advantageously between 5 and 180, preferably between 8 and 60; - halogenated organoaluminum compound / titanium compound, and possibly vanadium: greater than 1; it is preferably less than or equal to 6; compound capable of forming a magnesium halide in situ / compound of titanium, and optionally of vanadium: advantageously between 1 and 15, preferably between 1 and 6; vanadium compound / titanium compound: advantageously less than or equal to 6, preferably less than or equal to 3, more preferably between 0 and 1; - halogenated organoaluminum compound / compound capable of forming a magnesium halide in situ: advantageously between 0.3 and 2, preferably between 0.5 and 1.5.
• the catalyst thus obtained therefore comprises at least one titanium compound, at least one halogenated organo-aluminum compound and at least one inorganic magnesium compound suspended in at least one ⁇ , ⁇ -dihaloalkane; it is characterized in that the titanium compound is essentially a titanium (III) compound, the overall content of titanium (II) and titanium (IV) being less than or equal to 15% of the total content of titanium.
• the catalyst can also comprise all or part of the inert solvent used during its preparation (it may be desirable to partially evaporate the solvent to adjust the solid concentrations).
• the catalyst can also comprise the ⁇ -olefin used during its preparation, where appropriate in the at least partially polymerized state.
• the titanium valence states are determined by means of a 3-part redox assay.
• the first part calculates the content of (Ti 2+ + Ti 3+ ); it consists in oxidizing Ti 2+ to Ti 3+ by means of protons brought in the form of a 2N HCl solution prepared in degassed distilled water.
• the Ti 3+ formed plus the Ti 3+ originally present are then oxidized to Ti 4+ by means of an excess of 0.2N Fe 3+ solution.
• Fe 3+ is reduced to Fe 2+ which is determined by potassium dichromate in a sulfuric-phosphoric medium in the presence of 0.2% sodium diphenylamine sulfonate.
• the amount of Fe 2+ thus dosed corresponds to the Ti 2+ + Ti 3+ ions originally present in the catalyst.
• the second part calculates the content of 2Ti 2+ + Ti 3+ . It consists in oxidizing Ti 2+ and Ti 3+ by means of an excess of a solution of Fe 3+ ions, in the absence of protons to avoid the oxidation of Ti 2+ to Ti 3+ , according to the reactions:
• the determination of the Fe 2+ ion is then carried out using potassium dichromate as above.
• the value obtained corresponds to the sum 2Ti 2+ + Ti 3+ present in the catalyst.
• the third part makes it possible to determine the Ti 4+ content by reduction, by means of triethylaluminum according to an atomic ratio Al / Ti equal to 6, of the titanium (IV) present in titanium (III) and titanium (II).
• the assay is then carried out according to the first part above, the value found for Ti 2+ + Ti 3+ corresponding to the sum Ti 2+ + Ti 3+ + Ti 4+ of the ions present in the catalytic component analyzed and therefore to the total titanium content.
• the different percentages are calculated by solving the following system of equations:
• trihalides TiX 3 advantageously trichloride TiCl 3 .
• the catalyst according to the invention may also comprise at least one vanadium compound in the form of either trihalide VX 3 , for example trichloride VCl 3 , tetrahalogenide VX 4 , for example tetrachloride VCl 4 , oxy-tri - VOX 3 halide, for example VOCl 3 oxytrichloride, of (halo) vanadyl ester of formula VO (OR) n X 3 _ n in which X is a halogen, preferably chlorine, R is an alkyl radical having from 1 to 6 carbon atoms and n is between 1 and 3.
• the vanadium is present in the valence state (III) and / or (IV).
• the magnesium compound contained in the suspension state in the catalyst according to the invention is advantageously a magnesium halide, preferably anhydrous, for example anhydrous magnesium chloride.
• the catalyst prepared according to the process of the invention can be brought into contact with, and can therefore also comprise, an organometallic activator from groups I to III of the Periodic Table, generally at room temperature with stirring.
• the nature and the quantity of the activator are chosen according to the desired performances (activator more or less reducing, catalyst having a great initial activity or leading to a polymer of specific melt index, etc.).
• the amount of activator is nevertheless generally between 1 and 100 times the molar amount of transition metal compound.
• the activator is advantageously chosen from trialkylaluminiums AlR 3 , tetralkylaluminoxanes RR'Al-O-AIR '' R ''', monoalkylsilanolatodialkylaluminiums RSiH 2 -O-AlR'R''and their mixtures, alkyl radicals R, R ', R'',R'', identical or different, having from 1 to
• Examples include triethyl aluminum, tri-n-butylaluminium, tri-n-octylaluminium, tétraisobutylaluminoxane, methylsilanolatodiisobuty ⁇ - aluminum.
• Another object of the present invention relates to a process for the polymerization of olefins at a temperature of between 20 ° and 350 ° C approximately in the presence of a catalyst as described above.
• polymerization is meant homopolymerization, in particular of ethylene as well as copolymerization, in particular of ethylene and of at least one ⁇ -olefin having 3 to 8 carbon atoms.
• the polymerization process can be carried out at a temperature between 20 ° and 250 ° C, preferably between 150 ° and 250 ° C, under a pressure of up to about 200 bars, in solution or in suspension in a hydrocarbon inert having at least 6 carbon atoms such as a cut of C 10 -C 12 saturated aliphatic hydrocarbons.
• concentration of titanium compound in the catalyst used is preferably between 0.1 and 0.4 mol per liter.
• the polymerization of ethylene it can also be carried out, continuously, in a reactor in which the average residence time of the catalyst is between 1 and 150 seconds approximately, the polymerization being carried out at a temperature between 160 and 350 ° C approximately, under a pressure between 400 and 3000 bars approximately.
• the polymerization process according to the invention makes it possible to obtain a whole range of ethylene polymers with a density between 0.87 and 0.97.
• the copolymerization of a gas stream containing from 10 to 75% by weight of propylene and from 90 to 25% by weight of ethylene leads to a copolymer having a density of between 0.95 and 0.88 respectively.
• the copolymerization of a gas stream of ethylene (95 to 40% by weight) and butene-1 (5 to 60% by weight) makes it possible to obtain copolymers having a density of between 0.95 and 0.915 respectively.
• a gas stream containing from 30 to 70% by weight of ethylene and from 70 to 30% by weight of hexene-1 makes it possible to obtain a copolymer of density between 0.89 and 0.93 respectively.
• a terpolymer with a density of 0.88 to 0.915 can be obtained by terpolymerizing a gas stream containing respectively from 25% to 45% by weight of ethylene, and from 75% to 55% by weight of a mixture of propylene and butene. 1.
• the catalysts according to the invention show a high catalytic activity during the polymerization of ethylene.
• the nature of the activator it is possible to obtain catalytic systems having a large initial polymerization constant and / or which can lead to polymers having a melt index of between 0.2 and 20 dg / min.
• melt index of between 0.2 and 20 dg / min.
• the catalysts were prepared in a glass flask fitted with a stirrer and surmounted by a condenser, under a nitrogen atmosphere.
• the various reagents are introduced at a speed such that the reaction medium is maintained at a temperature between 15 and 60 ° C.
• the preparation lasts about an hour.
• DCE 1,2-dichloroethane
• hexene-1 hexene-1
• DCEA dichloroethylaluminium
• Example 3 The procedure of Example 3 was repeated, replacing the DCEA with tri (n-octyl) aluminum.
• Example 12 vanadium oxytrichloride is introduced simultaneously with titanium tetrachloride, before the introduction of DCEA.
• vanadium oxytrichloride is introduced simultaneously with titanium tetrachloride, before the introduction of DCEA.
• Example 3 The procedure of Example 3 was repeated, replacing the BEM mole by mole with the BOM.
• Example 15 The procedure of Example 3 was repeated, replacing mole to mole TiCl 4 with n-butyl titanate.
• Example 3 The procedure of Example 3 was repeated, replacing mole to mole VOCl 3 with VCl 4 (Example 16) or with vanadyl triisobutylate (Example 17).
• the catalyst obtained has a titanium (II) content equal to 57% of the total titanium content, while it is only 6.5% for the catalyst according to Example 4.
• the installation includes a 1 liter stirred autoclave reactor, thermostate and fitted with catalyst intake valves and withdrawal of the polyethylene formed.
• the polymerization is carried out discontinuously by first introducing the catalyst and the activator then by pressurizing the autoclave using ethylene up to a pressure of 6 bars. This pressure is maintained by adding fresh ethylene, the flow rate of which is measured. After a given reaction time, the quantity Q formed of polyethylene is weighed, expressed in grams per milliatome-gram of transition metal per minute and per ml -1 -1 of ethylene in Table II below.
• the activator is a mixture of triethylaluminum (25 mol%) and methylsilanolatodiisobutylaluminum (75 mol%) in an atomic ratio Al / Ti + V equal to 15.
• Examples 22bis, 37 and 38 are comparative.
• Example 4 The catalyst of Example 4 was used and, as activator, methylsilanolatodiisobutylaluminum alone according to one. Al / Ti ratio equal to 20. Under the polymerization conditions of Examples 20 to 38, 1700 g of polyethylene were obtained per milliatomegram of titanium, per minute and per mole.1 -1 of ethylene.
• Example 4 The procedure of Example 4 was repeated using n-butyl titanate (Ti (O-nBu) 4 ) in place of TiCl 4 . Under the polymerization conditions of Examples 20 to 38, using as activator methylsilanolatodiisobutylaluminum alone according to an Al / Ti atomic ratio equal to 20, 1600 g of polyethylene were obtained per milliatomegram of titanium, per minute and per mole.1 -1 d 'ethylene.
• Ti (O-nBu) 4 n-butyl titanate
• the copolymerization is carried out of a mixture of 40% ethylene, 35% propylene and 25% butene-1 (% by moles).
• the catalytic system comprises the catalyst of Example 3 and the triethylaluminum activator (25 mol%) - methylsilanolatodiisobutylaluminum (75 molar), the atomic ratio Al (of the activator) to the sum Ti + V (of the catalyst) being equal to 20.
• the catalyst contains at least one titanium compound, at least one halogenat organoaluminum compound and at least one inorganic magnesium compound in suspension in at least one ⁇ , ⁇ -dihalogeno kane;
• the titanium cmpound is essentially atitanium (III) compound, thetotal titanium (II) and titanium (IV) content being le than or equal 15% to thetotal titanium content.
• It may also contain at least one vanadium compound, an inert solvent, at lea one partiallypolymerized ⁇ -olefinand atleastone organometallic activatorfromgroups I to II ofthe PeriodicClassification. so described is a process for polymerization ofolefins in the presence ofsaid catalyst.
• the method comprises, in a first step, the reduction of a titanium compound (IV) in an ⁇ , ⁇ -dihalogénoalca by means of a molar excess of at least one halogenated organoaluminum compound, in the absence of a ether, then, in a second step, the addition to the reaction mixture of a compound capable of forming a halide of magnesium in situ, without further reduction of the titanium compound obtained during the first step.
• the catalyst comprises at least one titanium compound, at least one halogenated organo-aluminum compound, and at least one inorganic magnesium compound suspended in at least one ⁇ , ⁇ -dihaloalkane;
• the titanium compound is essentially a titanium (III) compound, the globa entitane (II) and entitane (IV) content being less than or equal to 15% of the total titanium content.
• It may further comprise in the ego a vanadium compound, an inert solvent, at least one ⁇ -olefin in the partially polymerized state and at least one organometallic activate from groups I to III of the Periodic Table. Process for the polymerization of olefins in the presence of the catalyst.
• a first step the reduction of a titanium (IV) compound in an ⁇ , ⁇ -dihalogenoalkane using a lar excess of at least one halogenated organoaluminium compound in the absence of an ether, and then in a second step, the ad tion of a reaction mixture of a compound capable of forming a magnesium halide in-situ, without additional reduction of the ti nium compound obtained in the first step.
• the catalyst contains at least one titanium compound, at least one halogenat organoaluminum compound and at least one inorganic magnesium compound in suspension in at least one ⁇ , ⁇ -dihalogeno kane;
• the titanium cmpound is essentially a titanium (III) compound, the total titanium (II) and titanium (IV) content being l than or equal 15% to the total titanium content.
• It may also contain at least one vanadium compound, an inert solvent, at le one partially polymerized -olefin and at least one organometallic activator from groups I to II of the Periodic Classification. so described is a process for polymerization of olefins in the presence of said catalyst.
• the method comprises, in a first step, the reduction of a titanium compound (IV) in an ⁇ , ⁇ -dihalogénoalca by means of a molar excess of at least one halogenated organoaluminum compound, in the absence of a ether, then, in a second step, the addition to the reaction mixture of a compound capable of forming a magnesium halide in situ, without additional duction of the titanium compound obtained during the first step.
• the catalyst comprises at least one titanium compound, at least one halogenated organo-aluminum compound, and at least one inorganic magnesium compound suspended in at least one ⁇ , ⁇ -dihaloalkane;
• the titanium compound is essentially a titanium (III) compound, the overall titanium (II) and titanium (IV) content being less than or equal to 15% of the total titanium content.
• It may further comprise in the ego a vanadium compound, an inert solvent, at least one ⁇ -olefin in the partially polymerized state and at least one organometallic activate from groups I to III of the Periodic Table. Process for the polymerization of olefins in the presence of the catalyst.

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• 1988
  • 1988-06-23 FR FR8808448A patent/FR2633299B1/fr not_active Expired - Fee Related
• 1989
  • 1989-06-22 CA CA000603628A patent/CA1340306C/fr not_active Expired - Fee Related
  • 1989-06-23 AT AT89401780T patent/ATE80401T1/de not_active IP Right Cessation
  • 1989-06-23 KR KR1019900700324A patent/KR0145290B1/ko not_active Expired - Lifetime
  • 1989-06-23 JP JP1507798A patent/JP2767754B2/ja not_active Expired - Lifetime
  • 1989-06-23 DE DE8989401780T patent/DE68902796T2/de not_active Expired - Lifetime
  • 1989-06-23 ES ES89401780T patent/ES2044168T3/es not_active Expired - Lifetime
  • 1989-06-23 WO PCT/FR1989/000321 patent/WO1989012649A2/fr active Application Filing
  • 1989-06-23 EP EP89401780A patent/EP0351266B1/fr not_active Expired - Lifetime
• 1992
  • 1992-12-08 GR GR920402828T patent/GR3006468T3/el unknown

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