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
  • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
• • 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
  • C08F4/65—Pretreating the metal or compound covered by group C08F4/64 before the final contacting with the metal or compound covered by group C08F4/44
• • 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
  • C08F4/65—Pretreating the metal or compound covered by group C08F4/64 before the final contacting with the metal or compound covered by group C08F4/44
  • C08F4/652—Pretreating with metals or metal-containing compounds
  • C08F4/654—Pretreating with metals or metal-containing compounds with magnesium 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
  • 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
  • C08F4/65—Pretreating the metal or compound covered by group C08F4/64 before the final contacting with the metal or compound covered by group C08F4/44
  • C08F4/652—Pretreating with metals or metal-containing compounds
  • C08F4/655—Pretreating with metals or metal-containing compounds with aluminium 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
  • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
  • C08F110/02—Ethene
• • 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
  • C08F2410/00—Features related to the catalyst preparation, the catalyst use or to the deactivation of the catalyst
  • C08F2410/06—Catalyst characterized by its size

Definitions

• the invention relates to a process for preparing a poly-1 -olefin in the presence of a Ziegler catalyst, one of whose components has been prepared from a magnesium alkoxide suspension and a transition metal compound.
• Magnesium alkoxides Mg(OR 1 J(OR 2 ) or "complex" magnesium alk ⁇ xides can be reacted with compounds of titanium, zirconium, vanadium or chromium to produce solids which together with organometallic compounds of group 1 , 2 or 13 of the Periodic Table (the groups are cited as printed, for example, in Handbook of Chemistry and Physics, 76 th edition (1995 - 1996)) give excellent catalysts for olefin polymerization.
• a process for the polymerization of ⁇ -olefins in the presence of a mixed catalyst whose component a has been prepared by reacting magnesium alkoxides with tetravalent, halogen-containing titanium compounds is known (cf. US-A 3,644,318).
• the magnesium alkoxides are used in the commercially available form.
• the polymers obtainable by this known process have a narrow molar mass distribution.
• a process for preparing a Ziegler catalyst in which a dissolved magnesium alkoxide is reacted with a halogen-containing Ti or V compound and a transition metal alkoxide (cf. EP-A 319 173).
• the catalyst particles formed are spherical and have a mean particle size of from 10 to 70 ⁇ m.
• WO 01/38405 describes a further process for reacting a gel-like dispersion of magnesium alkoxide with a transition metal compound to produce a Ziegler catalyst, in which the magnesium alkoxide is firstly milled dry to a particular mean particle size in a mill under inert conditions and is only then suspended in a suspension medium and converted into the gel-like, dispersion by stirring or shearing with a high-speed mixer.
• a further method of producing the gel-like dispersion of magnesium alkoxide is described in WO 03/99882, according to which the suspension of magensium alkoxide in a suspension medium is firstly subjected to heat treatment beyond a particular period of time and is then converted into the gel-like dispersion by stirring or shearing with a high-speed mixer.
• the catalyst should nevertheless display a very high polymerization activity over a long time, and the polymer prepared by means of the catalyst should have a particle size distribution which is just as narrow as polymer prepared in the presence of catalysts which are the result of complicated dispersion processes.
• the invention further relates to the catalyst obtainable by this process.
• This magnesium alkoxide can be a "simple" magnesium alkoxide of the formula Mg(OR 1 )(OR 2 ), where R 1 and R 2 are identical or different and are each an alkyl radical having from 1 to 6 carbon atoms. Examples are Mg(OC 2 Hs) 2 , Mg(OiC 3 H 7 ) 2 , Mg(OnC 4 Hg) 2 , Mg(OCH 3 )(OC 2 H 5 ), Mg(OC 2 H 5 )(OnC 3 H 7 ).
• a “complex” magnesium alkoxide can also be used.
• a “complex” magnesium alkoxide is a magnesium alkoxide comprising magnesium together with at least one metal of group 1 , 2, 13 or 14 of the Periodic Table. Examples of such a complex magnesium alkoxide are:
• the complex magnesium alkoxides (alkoxo salts) are prepared by known methods.
• magnesium alkoxides in particular Mg(OC 2 H 5 ) 2 , Mg(OnC 3 H 7 ) 2 or Mg(OiC 3 H 7 ) 2 .
• the magnesium alkoxide is used in pure form.
• the mean particle diameter is in the range from 600 to 700 //m, with at least 90% of the particles having a particle diameter in the range from 200 to 1400 ⁇ m.
• the commercial magnesium alkoxide having a mean particle diameter of from about 600 to 700 ⁇ m is, according to the invention, milled in the dry state in a mill under inert conditions until the milled material has a mean particle diameter, expressed as the d 50 , of less than 15 ⁇ m.
• a mill is considered to be under inert conditions when the proportion of gasses from the atmospheric environment in the total space of the milling apparatus which comes into contact with the magnesium alkoxide during milling has been reduced to less than 1 % by volume by displacement by inert gases.
• inert gases are, in particular, nitrogen, hydrogen and argon.
• Mills which are particularly suitable for the purposes of the present invention are, for example, ball mills, impact mills, opposed jet mills, spiral jet mills or air separation mills of the Ultra Rotor type.
• a particularly useful mill is an opposed jet mill as is described in the company brochure "Mechanischemaschinestechnik,r- and Nassvone" No. 017/10 297.2d from Hosakawa Alpine AG, Augsburg/Germany, and can also be procured from this company.
• the milled magnesium alkoxide having a mean particle diameter of less than 15 ⁇ m is, according to the invention, brought into suspension, i.e. uniformly distributed by stirring, in a vessel under inert conditions.
• a vessel is considered to be under inert conditions when the proportion of gases from the atmospheric environment in the total space of the vessel which comes into contact with the magnesium alkoxide during stirring has been reduced to less than 1% by volume by displacement by inert gases.
• Inert hydrocarbons which are suitable for the. purposes of the invention are aliphatic or cycloaliphatic hydrocarbons such as butane, pentane, hexane, heptane, isooctane, cyclohexane, methyicyciohexane, and also aromatic hydrocarbons such as toluene, xylene; it is also possible to use hydrogenated diesel oil fractions or petroleum spirit fractions which have carefully been freed of oxygen, sulfur compounds and moisture.
• the suspension is then immediately reacted in one stage or in a plurality of stages with a Ti compound (TiCI 4 , Ti(OR) 4 etc.), a Zr compound (Zr(OR) 4 etc.), a V compound (VCI 4 , VOCI 3 etc.) or a chromium compound (CrO 2 CI 2 etc.).
• the magnesium alkoxide suspension is reacted with the transition metal compound at a temperature in the range from 20 to 10O 0 C, preferably from 60 to 90 0 C, in the presence of an inert hydrocarbon while stirring at a stirrer speed corresponding to requirements.
• a temperature in the range from 20 to 10O 0 C preferably from 60 to 90 0 C
• an inert hydrocarbon while stirring at a stirrer speed corresponding to requirements.
• From 0.05 to 5 mol of transition metal compound preferably from 0.1 to 3.5 mol, are used per 1 mol of magnesium alkoxide.
• the reaction time is from 0.5 to 8 hours, preferably from 2 to 6 hours.
• the component a forms a suspension with the hydrocarbon (solid/liquid).
• the polymerization catalyst to be used according to the invention is prepared by combining the component a and an organometallic compound of a metal of group 1 , 2 or 13 of the Periodic Table (component b).
• component a can be reacted directly as a suspension with the component b, but it can also firstly be isolated as a solid, stored and resuspended for further use later.
• organoaluminum compounds Preference is given to using organoaluminum compounds as component b.
• Suitable . organoaluminum compounds include chlorine-containing organoaluminum compounds such as dialkylaluminum monochlorides of the formula R 3 2 AICI or alkylaluminum sesquichlorides of the formula R 3 3AI 2 CI 3 , where R 3 is an alkyl radical having from 1 to 16 carbon atoms. Examples which may be mentioned are (C 2 H 5 ) 2 AICI, CiC 4 Hg) 2 AICl, (C 2 H 5 ) 3 AI 2 CI 3 . It is also possible to use mixtures of these. compounds.
• organoaluminum compounds are chlorine-free organoaluminum compounds such as aluminum trialkyls AIR 3 3 or dialkylaluminum hydrides of the formi AIR 3 2 H, where R 3 is an alkyl radical having from 1 to 16 carbon atoms.
• Examples are AI(C 2 Hs) 3 , AI(C 2 Hg) 2 H, AI(C 3 H 7 ) 3 , AI(C 3 H 7 ) 2 H, AI(iC 4 H 9 ) 3 , AI(iC 4 H 9 ) 2 H, AI(C 8 Hi 7 J 3 , AI(C 12 H 25 )S, AI(C 2 H 5 )(C 12 H 2 S) 2 , AI(IC 4 H 9 )(C 12 H 2 S) 2 .
• organometallic compounds of metals of group 1 , 2 or 13 of the Periodic Table in particular mixtures of various organoaluminum compounds.
• AI(C 2 Hs) 3 and AI(JC 4 H 9 ) s AI(C 2 Hs) 2 CI and Al(C 8 Hi 7 ) 3 , AI(C 2 Hs) 3 and Al(C 8 H 17 ) 3 , AI(C 4 Hg) 2 H and AI(C 8 H 17 J 3 , AI(iC 4 H 9 ) 3 and AI(C 8 H 17 ) 3> AI(C 2 H 5 J 3 and Al(C 12 H 25 J 3 ,
• AI(JC 4 H 9 J 3 and AI(C 12 H 25 )S, AI(C 2 Hs) 3 and AI(C 16 H 33 ) 3 , AI(C 3 H 7 ) 3 and AI(C 18 H 37 J 2 (IC 4 H 9 ), AI(C 2 Hs) 3 and isoprenylaluminum ( reaction product of isoprene with AI(JC 4 Hg) 3 or AI(iC 4 H 9 ) 2 H).
• Mixing of the component a and the component b can be carried out prior to the polymerization in a stirred vessel at a temperature in the range from -30 to +150°C, preferably from -10 to +120 0 C. It is also possible to combine the two components directly in the polymerization vessel at a temperature in the range from 20 to 200 0 C.
• the addition of the component b can also be carried out in two steps, by the component a being preactivated with a first part of the compound b at a temperature in the range from -30 to +15O 0 C prior to the polymerization reaction and the further addition of a further part of the same component b or another component b being effected in the polymerization reactor at a temperature in the range from 20 to 200°C.
• ethylene is polymerized either alone or as a mixture of at least 90% by weight of ethylene and not more than 10% by weight of another 1 -olefin of the above formula.
• the polymerization is carried out in a known manner in solution, in suspension or in the gas. phase, continuously or batchwise, in one or more stages, preferably in two or three stages, at a temperature of from 20 to 200 0 C, preferably from 50 to 15O 0 C.
• the pressure is from 0.5 to 50 bar. Preference is given to carrying out the polymerization in the industrially particularly interesting pressure range from 1.5 to 30 bar.
• the component a or the reaction product of the component a with the component b is used in a concentration, based on transition metal, of from 0.0001 to 1 mmol, preferably from 0.001 to 0.5 mmol, of transition metal per dm 3 of dispersion medium.
• concentration based on transition metal, of from 0.0001 to 1 mmol, preferably from 0.001 to 0.5 mmol, of transition metal per dm 3 of dispersion medium.
• higher concentrations are also possible in principle.
• the suspension polymerization is carried out in an inert suspension medium customary for the Ziegler low-pressure process, for example in an aliphatic or cycloaliphatic hydrocarbon; examples of such a hydrocarbon are butane, pentane, hexane, heptane, isooctane, cyclohexane, methylcyciohexane. It is also possible to employ petroleum spirit fractions or hydrogenated diesel oil fractions which have carefully been freed of oxygen, sulfur compounds and moisture.
• Suspension polymerizations or gas-phase polymerizations can be carried out directly or after prepolymerization of the catalyst, with the prepolymerization advantageously being carried out by the suspension process.
• the molar mass of the polymer is regulated in a known manner; preference is given to using an appropriate amount of hydrogen for this purpose. Owing to the high activity of the catalyst used, the process of the invention gives polymers having a very low transition metal and halogen content and therefore extremely good results in the color stability test and corrosion test.
• the process of the invention surprisingly makes it possible to prepare the catalysts in such a way that their particle size distribution and, to a certain extent, also the particle shape of the polymer powder formed and particularly surprisingly also the polymerization activity and the response to hydrogen of the catalyst can be set optimally without prior dispersion of the Mg(OEt) 2 being necessary.
• An improved particle morphology especially a surprisingly narrow particle size distribution expressed as the S value in accordance with DlN 66 144, no coarse and fine fractions and high catalyst productivities are obtained according to the invention.
• the bulk densities are comparable to those of the prior art.
• the morphological properties of the polymer powder can be influenced, which brings with it valuable advantages for an industrial process in that the transport of the polymer powder in the plant is simpler and the powder flow is better.
• the high catalyst productivity gives lower residual catalyst contents in the product and thus improved quality.
• the preparation of the component a requires a lower amount of energy and a significantly shorter time.
• VN viscosity number
• the suspension of the solid was cooled to room temperature.
• the suspension of the solid was cooled to room temperature.
• the settling time of the resulting gel-like Mg(OC 2 H 5 ) 2 dispersion after switching off the stirrer was more than 30 minutes.
• This Mg(OC 2 H 5 ) 2 dispersion was brought to 70°C at a stirrer speed of 250 rpm and 0.06 mol Of TiCI 4 in 50 cm 3 of diesel oil (hydrogenated petroleum spirit fraction having a boiling range of 140 - 170 0 C) was metered in over a period of 4 hours.
• the mixture was then heated to 110 0 C and 0.14 mol Of AI 2 (C 2 Hs) 3 CI 3 in 100 cm 3 of diesel oil (hydrogenated petroleum spirit fraction having a boiling range of 140 - 170 0 C) was metered in over a period of 2 hours at a stirrer speed of 250 rpm.
• the temperature was subsequently maintained at 110 0 C for a further 2 hours.
• the polymerization experiments were carried out batchwise in a 200 dm 3 reactor. This reactor was equipped with an impeller stirrer and baffles. The temperature in the reactor was measured and automatically kept constant. The polymerization temperature was 85 ⁇ 1 °C.
• the polymerization reaction was carried out in the following manner:
• the reactor was pressurized a number of times to 8 bar with H 2 (hydrogen) and depressurized again in order to remove the nitrogen completely from the reactor (the procedure was monitored by measuring the H 2 concentration in the gas space of the reactor, which was finally 95% by volume).
• the polymerization was started by opening the ethylene inlet. Ethylene was introduced in an amount of 8.0 kg/h over the entire polymerization time, with the pressure in the reactor slowly increasing.
• the polymerization was stopped after 225 minutes (30 kg of ethylene introduced) and the total pressure was read off. The contents of the reactor were drained onto a filter. The polymer which was moist with diesel oil was dried for a number of hours in a 1.0 stream of nitrogen. The results of the polymerizations are shown in table 1.
• Comparison with comparative example 1 shows that a particle diameter higher than that 30 used according to the process of the invention produces a catalyst having a significantly lower activity and that the polymer has an unsatisfactory particle size distribution.
• Comparison with comparative example 2 and comparative example 3 shows that a costly dispersion step of 20 hours does not give an improved catalyst.

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• 2004
  • 2004-07-29 DE DE102004037229A patent/DE102004037229A1/de not_active Withdrawn
• 2005
  • 2005-07-27 WO PCT/EP2005/008127 patent/WO2006010599A1/en not_active Ceased
  • 2005-07-27 JP JP2007523005A patent/JP2008508376A/ja active Pending
  • 2005-07-27 CN CNB200580025162XA patent/CN100523015C/zh not_active Expired - Fee Related
  • 2005-07-27 US US11/658,808 patent/US7649061B2/en not_active Expired - Fee Related
  • 2005-07-27 KR KR1020077001985A patent/KR20070049144A/ko not_active Withdrawn
  • 2005-07-27 EP EP05766762A patent/EP1778743A1/en not_active Ceased

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