WO1991006577A1 - Adjuvant de support pour catalyseur de polymerisation ameliore a base de vanadium - Google Patents

Adjuvant de support pour catalyseur de polymerisation ameliore a base de vanadium Download PDF

Info

Publication number
WO1991006577A1
WO1991006577A1 PCT/US1990/006240 US9006240W WO9106577A1 WO 1991006577 A1 WO1991006577 A1 WO 1991006577A1 US 9006240 W US9006240 W US 9006240W WO 9106577 A1 WO9106577 A1 WO 9106577A1
Authority
WO
WIPO (PCT)
Prior art keywords
vanadium
catalyst
catalyst component
fluorine
support material
Prior art date
Application number
PCT/US1990/006240
Other languages
English (en)
Inventor
Anthony Nicholas Speca
Original Assignee
Exxon Chemical Patents Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Exxon Chemical Patents Inc. filed Critical Exxon Chemical Patents Inc.
Publication of WO1991006577A1 publication Critical patent/WO1991006577A1/fr

Links

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

Definitions

  • This invention relates to a catalyst component and a process for preparing said catalyst component.
  • the catalyst component may be employed with or without a cocatalyst in the polymerization of olefins to polyolefins.
  • the process for preparing the catalyst component comprises the fluoriding of a support and further reaction of the support with a vanadium compound to produce a novel catalyst component which allows the molecular weight distribution of the polyolefins to be controlled by controlling the amount of fluorination and the fluorination temperature.
  • vanadium-based catalysts in the polymerization of olefins is well known.
  • vanadium catalysts When unsupported, vanadium catalysts usually assume the form of an oil or gum, and tend to cause fouling of the polymerization reactor. As a consequence, unsupported vanadiu -based catalysts are unsuitable for use in a slurry or gas phase reaction process.
  • supported vanadium catalysts suffer from the fouling problem to a lesser degree.
  • supported vanadium catalysts suffer from a. series of shortcomings.
  • First, supported vanadium catalysts tend to produce polymers having too broad molecular weight distributions (MWD), with the polymer including a significant amount of low molecular weight oligomers. These oligomers, when present in polymers used in the manufacture of blow molded articles, produce an unacceptable amount of smoke.
  • MWD molecular weight distributions
  • a second shortcoming of supported vanadium catalysts is that these catalysts, when used in the polymerization of ethylene or in the copolymerization of ethylene with other 1-olefins, exhibit low activity in comparison to supported titanium-based catalysts. It would thus be desirable to have a supported vanadium catalyst which would have increased activity.
  • a third shortcoming of supported vanadium catalysts is their need for relatively high levels of hydrogen 5 during polymerization to control resin molecular weight. It would be desirable to have a supported vanadium catalyst that would have increased response to hydrogen for effecting chain termination and controlling molecular weight. 0 Finally, supported vanadium catalysts require relatively high levels of comonomer to prepare medium and low density resins. It would be desirable to have a supported vanadium catalyst which would have increased response to comonomer to effect resin density reduction. 15 Good comonomer utilization means that less comonomer is needed to give the target resin density. This is important for both slurry and gas phase polymerization since large amounts of comonomer lead to upsets in process conditions by increasing the solubilizing power of the 2.0 slurry diluent or forming droplets in the gas phase.
  • fluorided supports can be used to advantage with chromium catalysts.
  • fluorination increases chromium catalyst activity, narrows resin MWD, but decreases resin melt indices. Decreases in 25 resin melt index (MI) are indicative of increased molecular weight and decreased response of the catalyst to hydrogen.
  • U.S. Pat. No. 4,359,403 teaches the addition of fluorine-containing compounds to silica prior to or during heating for the sole purpose of improving the activity of the silica supported catalyst.
  • the catalyst is prepared by reacting the fluorided silica with a magnesium compound and then with the active metal.
  • the patent also teaches the addition of alcohol for the purpose of improving the catalyst response to hydrogen. No mention is made of improved hydrogen response or comonomer response caused by the fluorination, nor is any mention made of the ability to control molecular weight distribution through independent control of the amount of fluorination and the fluorination temperature.
  • This invention discloses a novel vanadium-based catalyst component and a method for producing said catalyst component.
  • the catalyst component when used alone or in conjunction with a cocatalyst, provides a catalyst system having unique properties for olefin polymerization, including increased catalytic activity, increased response to hydrogen for chain termination, and increased response to comonomer for controlling resin density.
  • the catalyst system of the invention provides the ability to control the molecular weight distribution through independent control of the amount of fluorination and the temperature at which the support is fluorinated.
  • fluorination of supports for vanadium-based catalysts has the effect of increasing catalyst activity and narrowing MWD's
  • fluorination also, unexpectedly, has the effect of increasing resin melt indices, i.e. increasing hydrogen response.
  • fluorination in accordance with the present invention decreases resin density which is indicative of increased comonomer response.
  • this catalyst system to control the MWD of the polymer product through fluorination substantially eliminates the formation of low weight oligomer thereby reducing * the amount of smoke and facilitating the use of a poll -.efin resin produced by the catalyst system as a blow molding resin.
  • the flexibility provided by this catalyst in allowing the tailoring of the breadth of the MWD over a wide range of molecular weights by varying the extent of fluorination and/or the fluorination temperature, permits the production of polymers having properties optimally suited for specific applications.
  • the catalyst component disclosed in this invention may be used alone or in combination with an alky aluminum cocatalyst under conditions characteristic of Ziegler polymerization.
  • the process for producing this novel catalyst component comprises the steps of dry mixing a support material with a fluorine compound. The mixture is then heated to some desirable fluorination temperature. Next, the support material is treated with a vanadium compound.
  • the catalyst component of this invention may be used to produce polymer having a desired MWD by judiciously selecting the fluorine content and the fluorination temperature.
  • the support material is selected from the group consisting of silica, alumina, silica-alumina mixtures, talc, zirconia, thoria, and metal oxides from the metals of Group IIA, IVA and IVB of the Periodic Table of the Elements.
  • the fluorine compound is selected from the group consisting of (NH 4 ) 2 SiFg, NH 4 F NH 4 HF H 4 BF 4 , KF, A1F 3 , HF, Zn(BF 4 ) 2 , Ni(BF 4 > 2 , Sn(BF 4 )' 2 , (NH 4 ') 2 TiF 6 and the like.
  • the disclosed catalyst may be employed, either by itself or in conjunction with a cocatalyst, in the gas phase, high pressure, solution, or slurry processes for the production of polyolefin resins.
  • the catalyst may be usefully employed in the polymerization of ethylene and other alpha-olefins, particularly alpha-olefins having from 3 to 8 carbon atoms and in the copolymerization of 5 these with other 1-olefins or diolefins, such as propylene, butene, pentene and hexene, butadiene, 1,4-pentadiene, and the like, so as to form copolymers of low and medium densities.
  • the catalyst is particularly useful for the polymerization of ethylene and the 0 copolymerization of ethylene with other alpha-olefins in gas phase processes to produce HDFE or LLDPE.
  • the catalyst component of the present invention comprises the solid reaction product of (A) a fluorine 5 compound in the presence of an inert support material, (B) a vanadium compound, (C) an optional halogenating agent, and (D) an optional reducing agent.
  • the catalyst component may optionally be reacted with (E) an organoaluminum compound cocatalyst to form a catalyst system.
  • the order of addition of ingredients in forming the vanadium containing catalyst can vary.
  • the silica support material is dry mixed with the ammonium silicofluoride fluorine compound.
  • Both the silica and the ammonium silicofluoride are solid particulates. Dry mixing is accomplished by simply blending the two solids.
  • the fluorine compound could be dissolved in water and sprayed onto the dry silica, or the fluorine compound could be dissolved in water and added to an aqueous suspension of the silica, or the dry fluorine compound could be added to an aqueous suspension of the silica.
  • dry blending is preferred. The mixture is then heated to a desirable temperature. The amount of fluorine used and the temperature to which the mixture is raised influence the narrowness of the MWD of the polymers formed using the catalyst of this invention.
  • the support material can be any of the solid particulate porous supports such as talc, silica, zirconia, thoria, magnesia, and titania.
  • the support material is a Group IIA, IIIA, IVA and IVB oxide in finely divided form.
  • Suitable inorganic oxide materials which are desirably employed in accordance with this invention include silica, alumina, and silica-alumna and mixtures thereof, with silica being most preferred.
  • Other inorganic oxides that may be employed either alone or in combination with the silica, alumina, or silica-alumina are magnesia, titania, zirconia, and the like.
  • the preferred fluorine compound is ammonium silicofluoride (ASF), ( H 4 ) 2 SiF ⁇ , but many other fluorine containing compounds may be used.
  • fluorine compounds which may be used are hydrogen fluoride, HF, fluorides of ammonium and metals, such as KF, KF.HF, NH ⁇ F, NH.F.HF, A1F 3 , complex fluorides of ammonium and metals, such as (NH 4 ) 2 SiF 6 , H 4 BF 4 , Zn(BF 4 ) 2 , (NH 4 ) 2 TiF 6 , Ni(BF 4 ), Sn(BF 4 ) 2 and the like.
  • the fluorine treated support, slurried in a hydrocarbon, is treated with a vanadium compound.
  • the preferred vanadium compounds which may be usefully employed in the preparation of the catalyst component of this invention are well known in the art and may be represented by the formulas:
  • R is a hydrocarbon
  • R preferably represents a C ⁇ to C
  • vanadium compounds are vanadyl trichloride, vanadium tetrachloride, vanadium tetrabutoxide, alkoxy vanadium chloride, vanadium trichloride, vanadyl acetylacetonate, vanadyl dichloroacetylacetonate, vanadyl chlorodiacetylacetonate, vanadium trichloride complexed with tetrahydrofuran, vanadyl tribromide, vanadium- tetrabromide, and the like.
  • the vanadium compound is preferably added to the reaction mixture in the form of a solution.
  • the solvent can be any of the well-known inert hydrocarbon solvents such as hexane, heptane, benzene, toluene, and the like.
  • the optional halogenating agents are employed to obtain increased catalytic activity.
  • the halogenating agents may be used to increase activity without detrimentally affecting the molecular weight distributions obtainable in accordance with this invention in which the content of the oligomer is reduced.
  • the halogenating agents which can be employed are chlorinating, brominating and iodinating agents.
  • the halogenating agents are desirably strong halogenating agents although weaker halogenating agents may be used.
  • the halogenating agents can be liquid or gaseous under the reaction conditions.
  • Illustrative but non-limiting examples of the strong halogenating agents that can be usefully employed in accordance with this invention are the silicon halides and the hydro
  • silicon compounds are silicon tetrachloride, silicon tetrabromide, chlorosilanes such as, for example, trichlorosilane, trimethylchlorosilane, dimethyldichlorosilane, ethyltrichlorosilane, diethyldichlorosilane, dichlorodibutylsilane, trichlorobutylsilane, tribromobutylsilane, bromotrimethylsilane, and the like.
  • chlorosilanes such as, for example, trichlorosilane, trimethylchlorosilane, dimethyldichlorosilane, ethyltrichlorosilane, diethyldichlorosilane, dichlorodibutylsilane, trichlorobutylsilane, tribromobutylsilane, bromotrimethylsilane, and the like.
  • halogenating agents are the hydrocarbyl halides which include carbon tetrachloride, chloroform, 1,1,1-trichloroethane, dichloromethane, trichlorofluormethane, and the like.
  • the preferred halogenating agents are strong • activating chlorinating agents, among which the most preferred are silicon tetrachloride, trichlorofluoromethane, trichloroethane, and the like.
  • Illustrative of weak activating chlorinating agents are the thionyl halides, such as SOCl 2 .
  • the halogenating agent may be conveniently added to the reaction slurry consisting of the reaction product of the fluorided support material, the vanadium compound, and the organoaluminum compound.
  • the halogenating agent may be added as a pure compound or in the form of a solution with an inert solvent such as, for example, an aliphatic hydrocarbon solvent or an aromatic hydrocarbon solvent, or int may be added as a gas.
  • the slurrying of the support material is conducted in an inert solvent.
  • the inert solvent can be the same as that employed to dissolve the individual ingredients prior to the treatment step.
  • Preferred solvents include mineral oils and the various hydrocarbons which are liquid at reaction temperatures and in which the individual ingredients are soluble.
  • the amount of solvent used is not critical. The amount employed should, however, be sufficient to provide adequate capability for heat transfer away from the catalyst components during reaction and to permit good mixing.
  • the catalyst component may optionally be reacted with a reducing agent.
  • the reducing agent can be represented by the general formula Rl m A1X 3_ m wherein R' represents an alkyl group, cycloalkyl group or aryl group, X represents a halogen atom and "m" represents a suitable numeral equal to or greater than 1 and less than or equal to 3, or mixtures or complex compounds thereof.
  • R' represents an alkyl group, cycloalkyl group or aryl group
  • X represents a halogen atom
  • "m" represents a suitable numeral equal to or greater than 1 and less than or equal to 3, or mixtures or complex compounds thereof.
  • alkyl aluminum halide compounds wherein the alkyl groups have from 1 to 18 carbon atoms, preferably 1 to 9 carbon atoms and the halogen is chlorine.
  • organoaluminum compounds which may be suitably employed are the trialkylaluminums such as trimetylaluminum, triethylaluminum, tributylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, and the like.
  • diaklyaluminum halides are diethylaluminum chloride, diethylaluminum fluoride, dimethylaluminum chloride, dibutylaluminum chloride, diethylaluminum bromide, diethyaluminum iodide and dibutylaluminum iodide.
  • Examples of the monoalkylaluminum dihalides are methylaluminum dichloride, ethylaluminum dichloride, butylaluminum dichloride, isobutylaluminum dichloride, ethylaluminum dibromide, ethylaluminum diiodide, butylaluminum dibromide, and butylaluminum diiodide.
  • the sesquihalides can be suitably employed such as methylaluminum sesquichloride and ethylaluminum sesquichloride and the like.
  • isobutylaluminum dichloride is used.
  • the alkylaluminum may conveniently be added to the agitated slurry containing the particulate supports in the form of a solution with a dry hydrocarbon such as hexane, benzene, toluene, and the like. Alternatively, the alkylaluminum may be added to the slurry in undiluted form.
  • the amounts of catalytic ingredients employed in the preparation of the supported catalyst component can vary over a wide range.
  • the fluorine containing compound is -12- added to the support at a concentration of about .01 to 1.0 millimoles F/g of dried support, preferably in the range of about 0.1 to about 0.6 millimoles F/g of dried support and especially in the range of about 0.2 to 0.4 millimoles F/g of dried support.
  • the precise amount of fluorine containing compound added directly affects the narrowness of the MWD of the resulting polyolefins formed using the catalyst and must be judiciously selected to effect MWD's of desired breadth.
  • the reaction of the support material with the fluorine containing compound takes place at temperatures of from 200°C to 1000°C, preferably from 350°C to 800°C.
  • the precise temperature to which the mixture is heated directly affects the narrowness of the MWD of the resulting polyolefins formed using the catalyst and must be judiciously selected to effect MWD's of desired narrowness.
  • the vanadium compound is added to the slurry of inert support at a concentration of about 0.05 to 2.0 millimoles V/g of dried support, preferably in the range of about 0.1 to about 1.5 millimoles V/g of dried support and especially in the range of about 0.2 to 1.0 millimoles V/g of dried support.
  • reaction steps may be conducted at temperatures in the range of about -50°C to about 150°C.
  • Preferred temperature ranges are from about -30°C to about 60°C with -10°C to about 50°C being most preferred.
  • the catalyst components prepared in accordance with this invention are usefully employed with cocatalysts well known in the art of the Ziegler catalysis for polymerization of olefins.
  • the cocatalysts which are used together with the transition metal containing catalyst component are organometallic compounds of Group la, Ila and Ilia metals such as aluminum alkyl ⁇ , aluminum alkyl hydrides, lithium aluminum alkyl ⁇ , zinc alkyls, magnesium alkyls and the like.
  • the cocatalysts preferably used are the organoaluminuro compounds.
  • the preferred alkylaluminum compounds are represented by the formula A -*- R, n ⁇ l 3_ n wherein R f is hydrogen, hydrocarbyl or substituted hydrocarbyl group and n is as defined herein above.
  • R 1 is an alkyl group having from 2 to 10 carbon atoms.
  • X 1 is halogen and preferably chlorine.
  • Illustrative examples of the cocatalyst material are ethyl aluminum dichloride, ethyl aluminum sesquichloride, diethyl aluminum chloride, aluminum triethyl, aluminum tributyl, diisobutyl aluminum hydride, diethyl aluminum ethoxide and the like.
  • Aluminum trialkyl compounds are most preferred with triisobutylaluminum and aluminum triethyl being highly desirable.
  • Cocatalysts are added to the polymerization reactor at a molar ratio to V of about 50 to 250 however, greater or lesser amounts can be usefully employed.
  • the Al/V ratio is in the range of about 50 to about 150 and especially in the range of about 75 to 100.
  • the polymerization activators are preferably chlorocarbon activators.
  • the . activators are generally added to the polymerization reactor as a separate component. However, in the alternative, the activator can be adsorbed onto the surface of the catalyst component of this invention.
  • the activator serves to significantly increase the productivity of the catalyst.
  • Illustrative but non-limiting examples of the chlorocarbons are CHC1 3 , CFC1 3 CH 2 C1 2 , 0 ethyltrichloroacetate , methyltrichloroacetate, hexachloropropylene , butylperchlorocrotonate,
  • the activators may be gases or liquids at the conditions of polymerization.
  • the catalyst system comprising the organoaluminum cocatalyst and the vanadium-containing solid catalyst component of this invention is preferably employed for the polymerization of ethylene. However, this catalyst system can also be used to polymerize other alpha-olefins having from 3 to 20 carbon atoms, ethylene copolymers with other alpha-olefins or diolefins, and ethylene copolymers with other alpha-olefins or diolefins.
  • the catalyst system may be usefully employed to produce polyethylene or copolymers of ethylene.
  • the catalyst is especially useful for the preparation of resins for blown film and blow molding applications.
  • the olefins can be polymerized in the presence of the catalysts of this invention by any suitable known process such as, for example, suspension, solution and gas-phase processes.
  • the polymerization reaction employing catalytic amounts of the above-described supported catalyst can be carried out under conditions well known in the art of Ziegler polymerization, for example, in an inert diluent at a temperature in the range of 50°C to 120°C and a pressure of 1 to 40 atmospheres in the gas phase at a temperature range of 70°C to 100°C at about 1 atmosphere to 50 atmospheres and upward.
  • Illustrative of the gas-phae processes are those disclosed in U.S. Pat. No. 4,302,565 and U.S. Pat. No. 4,302,566, which references are hereby incorporated in their entirety by reference.
  • one advantageous property of the catalyst system of this invention is the reduced amount of gas phase reactor fouling.
  • the catalyst system can also be used to polymerize olefins at single phase conditions, i.e., 150°C to 320°C and 1,000-3,000 atmospheres. At these conditions the catalyst lifetime is short but the activity sufficiently high that removal of catalyst residues from the polymer is unnecessary. However, it is preferred that the polymerization be done at pressures ranging from 1 to 50 atmospheres, preferably 5 to 25 atmospheres.
  • the catalyst system of this invention is highly responsive to hydrogen, allowing for the close control of molecular weight.
  • Other well known weight controlling agents such as diethyl zinc, may in addition be employed.
  • the polymers prepared in accordance with this invention can be extruded, mechanically melted, cast or molded as desired. They can be used for plates, sheets, films, and a variety of other articles.
  • the silica support was prepared by placing Davison Chemical Company MS 948 microspheroidal silica having a pore volume of 1.7 cc/g
  • the polymers produced by the catalyst of this invention are characterized as having "controlled" MWD.
  • the polymer MWD is independently controlled by adjusting the amount of fluoride and the temperature to which the support and the fluorine containing compound are heated.
  • MWD is of critical importance. While it is possible to measure MWD directly, a less expensive but less direct method involving melt flow properties is used. Mel indices have successfully been used to characterize polymer MWD. Melt index ratio
  • MIR melt indices
  • Examples 1-3 illustrate the performance of known supported vanadium catalysts which do not incorporate the MWD regulating mechanisms of the instant invention. Specifically, Examples 1-3 relate to catalyst components produced with supports which have not been fluorided. Preparation of Catalytic Component The silica support was dehydrated by heating as described above without the addition of fluoriding agents. The catalyst component was prepared by suspending about 2 g of the support in about 30 cc of isopentane. A solution of V0Cl 3 in hexane (0.7 millimoles V/cc) was slowly added to the slurry while stirring to load 0.42 millimole V/g support.
  • Polymerization of ethylene took place in a bench scale reactor using 1,000 cc isobutane as the diluent. 1.5 cc Freon-11 was used as the promoter and 2.4 millimoles TEAL as the cocatalyst. Polymerization temperature was 80°C and polymerization time was 40 minutes. The concentration of ethylene used was 1.16 molar, the hydrogen to ethylene molar ratio was 0.026, and the hexene-1 to ethylene molar ratio was 0.36. The relatively large charge of hexene-1 was used to approximate the resin densities needed for film applications.
  • Unfluorided silica supports were prepared for Examples 1, 2, and 3 by dehydrating at 300°C, 500°C, and 800°C, respectively.
  • the polymerization results are shown in the first three columns of Table 1. Comparison of the three unfluorided examples shows that the dehydration temperature has little or no effect on resin melt flow properties. No effect on catalyst productivity was found at 500°C and 800°C. Lower productivity was observed when the catalyst was supported on the silica which had been dehydrated at 300°C. This was expected in view of the high hydroxyl content of the support and the known sensitivity of the Ziegler-Natta catalysts to acidic hydrogen.
  • Examples 4-6 illustrate the performance of catalyst which incorporates the MWD regulating mechanisms of the instant. Specifically, Examples 4-6 relate to catalyst 0components produced with supports which have been fluorided. Preparation of Catalytic Component
  • the silica support was heated as described for Examples 1-3 following the addition and stirring of 5ammonium silicofluoride into the support.
  • the mixture prior to dehydration was 2 wt% ammonium silicofluoride.
  • the catalyst component was prepared as in Examples 1-3. Polymerization
  • Example 1-3 Polymerization of ethylene took place in a bench scale reactor as for Example 1-3.
  • the molar concentration of ethylene, the hydrogen to ethylene molar ratio, and the hexene-1 to ethylene ratio were the same as in Examples 1-3.
  • Fluorided silica supports were prepared for Examples 4, 5, 6, and 7 by dehydrating at 350°C, 500°C, 650°C, and 800°C, respectively.
  • the polymerization results are shown in the last four columns of Table 1. Comparison of the four fluorided examples shows that the dehydration temperature has marked effect on productivity.
  • Productivity increased from 79 g PE/g catalyst for dehydration at 350°C (Example 4) to 139 g PE/g catalyst for dehydration at 800°C (Example 7).
  • the productivity for the fluorided catalyst dehydrated at 350° C (Example 4) approximately equalled the productivity of the unfluorided catalyst dehydrated at 500°C and 800°C, Examples 2 and 3, respectively.
  • the silica support in Examples 8-10 were dehydrated by heating as described above without the addition of fluoriding agents.
  • the catalyst components for Examples 8 and 9 were prepared as described in Examples 1-3 above.
  • the catalyst component for Example 10 was similarly prepared but with higher loadings. Specifically, the catalyst in Example 10 was loaded to 0.77 millimoles V, 1.34 millimole Al, and 4.8 millimole Si/g support.
  • the 5 fluorided supports (Examples 11-15) were prepared as in Examples 4-7 above.
  • the catalyst was made as described in Examples 4-7 above. Polymerization
  • Polymerization of ethylene took place in bench scale 0 reactors using 1,000 cc isobutane as the diluent. Polymerization temperature was 80°C and polymerization time was 40 minutes. Promoter and cocatalyst were the ⁇ ame as previous examples.
  • the molar concentration of ethylene used was 1.17, the hydrogen to ethylene molar ratio was 0.039, and the hexene-1 to ethylene ratio was 0.080.
  • the relatively small charge of hexene-1 was used to approximate the resin density needed for blow molding applications.
  • Examples 16-21 illustrate the effect of the amount of fluorination applied to the catalyst supports.
  • Preparation of Catalytic Component The silica support for Example 16 was dehydrated as described above to a temperature of 800°C.
  • the silica support for Examples 17-21 were fluorinated by heating as described above to a temperature of 650°C in the presence of various amounts of ammonium silicofluoride, ranging from 0.5 to 3.0 wt%, or 0.3 to 1.8 wt% F added.
  • the catalyst components for Examples 16-21 were prepared as described in Examples 4-7 above.
  • the catalyst was made as described in Examples 4-7 above.
  • Polymerization 5 Polymerization of ethylene took place in a bench scale reactor using 1,000 cc isobutane as the diluent. Polymerization temperature was 80°C and polymerization time was 40 minutes. Promoter and cocatalyst were the same as previous examples. The molar concentration of 0 ethylene used was 1.25, the hydrogen to ethylene molar -22- ratio was 0.014, and the hexene-1 to ethylene molar ratio was 0.33.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)

Abstract

L'invention se rapporte à un composant catalytique à base de vanadium utilisé pour la polymérisation d'1-oléfines et à un procédé de production d'un tel composant catalytique. On prépare ce composant catalytique en fluorurant un support. L'utilisation de ce composant catalytique fournit une réaction catalytique avec action accrue, avec meilleure réponse à l'hydrogène pour les terminaisons de chaînes, avec meilleure réponse aux comonomères pour la réduction de la densité de résines, et permet de réguler de façon indépendante la répartition du poids moléculaire des polymères en régulant la grandeur de la fluorination et la température de fluorination.
PCT/US1990/006240 1989-11-01 1990-11-01 Adjuvant de support pour catalyseur de polymerisation ameliore a base de vanadium WO1991006577A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US43069689A 1989-11-01 1989-11-01
US430,696 1989-11-01

Publications (1)

Publication Number Publication Date
WO1991006577A1 true WO1991006577A1 (fr) 1991-05-16

Family

ID=23708631

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1990/006240 WO1991006577A1 (fr) 1989-11-01 1990-11-01 Adjuvant de support pour catalyseur de polymerisation ameliore a base de vanadium

Country Status (2)

Country Link
AU (1) AU6725790A (fr)
WO (1) WO1991006577A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6368999B1 (en) 1998-08-26 2002-04-09 Exxon Mobil Chemical Patents Inc. Highly active supported catalyst compositions

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3130188A (en) * 1960-10-07 1964-04-21 Phillips Petroleum Co Catalyst and process for producing olefin polymers
GB1391772A (en) * 1971-01-26 1975-04-23 Bp Chem Int Ltd Polymerisation process
DE2146686B2 (de) * 1970-10-08 1979-01-18 Solvay & Cie., Bruessel Verfahren zur Polymerisation von Äthylen und Katalysator zur Durchführung dieses Verfahrens
US4262105A (en) * 1970-10-20 1981-04-14 Solvay & Cie Process for the polymerization of olefins and catalytic products
DE3212868A1 (de) * 1981-04-13 1982-10-28 Chemplex Co., 60008 Rolling Meadows, Ill. Olefin-polymerisations- und copolymerisations-katalysatoren, deren herstellung und damit durchgefuehrte polymerisationsverfahren

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3130188A (en) * 1960-10-07 1964-04-21 Phillips Petroleum Co Catalyst and process for producing olefin polymers
DE2146686B2 (de) * 1970-10-08 1979-01-18 Solvay & Cie., Bruessel Verfahren zur Polymerisation von Äthylen und Katalysator zur Durchführung dieses Verfahrens
US4262105A (en) * 1970-10-20 1981-04-14 Solvay & Cie Process for the polymerization of olefins and catalytic products
GB1391772A (en) * 1971-01-26 1975-04-23 Bp Chem Int Ltd Polymerisation process
DE3212868A1 (de) * 1981-04-13 1982-10-28 Chemplex Co., 60008 Rolling Meadows, Ill. Olefin-polymerisations- und copolymerisations-katalysatoren, deren herstellung und damit durchgefuehrte polymerisationsverfahren

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6368999B1 (en) 1998-08-26 2002-04-09 Exxon Mobil Chemical Patents Inc. Highly active supported catalyst compositions
US6524988B2 (en) 1998-08-26 2003-02-25 Exxonmobil Chemical Patents Inc. Highly active supported catalyst compositions
US6664348B2 (en) 1998-08-26 2003-12-16 Exxonmobil Chemical Patents Inc. Highly active supported catalyst compositions
US6667272B2 (en) 1998-08-26 2003-12-23 Exxonmobil Chemical Patents Inc. Highly active supported catalyst compositions
US6846770B2 (en) 1998-08-26 2005-01-25 Exxonmobil Chemical Patents Inc. Highly active supported catalyst compositions

Also Published As

Publication number Publication date
AU6725790A (en) 1991-05-31

Similar Documents

Publication Publication Date Title
US4607019A (en) Polymerization catalyst, production and use
US5064796A (en) Support adjuvant for improved vanadium polymerization catalyst
EP0133383B1 (fr) Catalyseur supporté pour la polymérisation de l'éthylène à température élevée
EP0117929B1 (fr) Polymérisation des alpha-oléfines, composant de catalyseur et système catalytique utilisant celui-ci
US4579835A (en) Polymerization catalyst, production and use
EP0447722B1 (fr) Catalyseur à base de zirconium pour la polymérisation d'oléfines
US4562170A (en) Polymerization catalyst
US4981826A (en) Polymerization catalyst prepared with a halogenated silane compound
US4554265A (en) Polymerization catalyst
EP0272132B1 (fr) Catalyseur pour polymérisation d'oléfines, sa production et son utilisation
US4634751A (en) Polymerization catalyst, production and use
EP0123510B1 (fr) Préparation de catalyseur de polymérisation des oléfines et leur utilisation
CA1216398A (fr) Poly er sa ion de l'ethylene
EP0435627B1 (fr) Catalyseur supporté pour polymérisation d'oléfines
US4618660A (en) Polymerization catalyst
US4626520A (en) Polymerization catalyst, production and use
EP0375199B1 (fr) Catalyseur supporté à base de vanadium pour la préparation de polyoléfines de distribution de poids moléculaire contrôlé
EP0373785A1 (fr) Catalyseur homogène ou supporté à base de vanadium pour polymérisation d'oléfines
WO1991006577A1 (fr) Adjuvant de support pour catalyseur de polymerisation ameliore a base de vanadium
JP2832753B2 (ja) 低オリゴマー含量及び高メルトインデックス比の高密度ポリエチレンの製造方法
EP0173486A1 (fr) Catalyseur de polymérisation, sa préparation et son utilisation
US5262372A (en) Supported vanadium catalyst for prodution of polyolefins of controlled molecular weight distribution
EP1502924A1 (fr) Catalyseurs pour la préparation de polyéthylène ayant une activité élevée préparés avec des composés phosphates et/ou phosphites

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU CA JP

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IT LU NL SE

NENP Non-entry into the national phase

Ref country code: CA