WO2000042077A1 - Procede de transfert d'un materiau polymere dans un reacteur a phase gazeuse - Google Patents

Procede de transfert d'un materiau polymere dans un reacteur a phase gazeuse Download PDF

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Publication number
WO2000042077A1
WO2000042077A1 PCT/FI2000/000032 FI0000032W WO0042077A1 WO 2000042077 A1 WO2000042077 A1 WO 2000042077A1 FI 0000032 W FI0000032 W FI 0000032W WO 0042077 A1 WO0042077 A1 WO 0042077A1
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Prior art keywords
liquid medium
reactor
polymer
gas phase
liquid
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PCT/FI2000/000032
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English (en)
Inventor
Ali Harlin
Henrik Andtsjö
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Borealis Technology Oy
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Priority to AU22961/00A priority Critical patent/AU2296100A/en
Publication of WO2000042077A1 publication Critical patent/WO2000042077A1/fr

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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
    • C08F297/00—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer
    • C08F297/06—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the coordination type
    • C08F297/08—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the coordination type polymerising mono-olefins
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2435—Loop-type reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/04—Polymerisation in solution
    • C08F2/06—Organic solvent
    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/34—Polymerisation in gaseous state
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • 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

Definitions

  • the present invention relates to polymer production and concerns a method for transferring polymer from a liquid slurry reactor to a gas phase reactor in a multistage polymerization process.
  • the invention can be used especially in polyolefin production.
  • Polymers are often prepared in a multistage process in order to provide desired properties. Especially molecular weight d stribution can thus be controlled.
  • the process may comprise, for example, a liquid phase polymeration and thereafter a gas phase polymerization.
  • Such two-stage processes have been used especially for preparing polyole ins, such as polyethylene.
  • US-A-4368291 discloses a process for preparing polyethylene, in which ethylene is first polymerized in a liquid reactor and thereafter in a gas phase reactor. Liquid hydrocarbon is used as a medium in the first stage, and the liquid medium and polymer together are transferred to the second stage. Dispersion medium from the gas phase reactor can be removed and cooled, possibly condensed, and recycled into the reactor. This provides an effective method to control the temperature in the reactor.
  • One disadvantage of this process is that the medium of the first stage may disturb the polymerization reactions in the second stage. For example, hydrogen from the first stage may be harmful in the second stage.
  • US-A-4692501 discloses a two-stage polymerization process where the first stage is conducted as a slurry polymerization in a continuous stirred tank reactor and the second stage is conducted in a gas phase reactor. Between the reactors there is an liquid exchanging stage. The slurry from the first polymerization stage is introduced into the top of the liquid medium exchanging zone and fresh liquid is introduced into the bottom of liquid exchanging stage. The slurry containing the fresh liquid and the polymer is then collected from the bottom of the zone and introduced into a gas phase reactor. The slurry medium from the first polymerization stage is collected from the top of the zone. The amount of fresh liquid introduced into the bottom is such that the volume of liquid discharged with the polymer from the liquid exchanging zone is 1 to 8 times, preferably 1.05 to 1.5 times the volume of the fresh liquid.
  • WO-A-92/12182 (based on FI-A-906428) discloses a two-stage process for preparing polyethylene, in which the first stage is a liquid phase polymerization in a loop reactor.
  • the polyethylene powder prepared in the first polymerization stage is separated from the liquid phase containing the diluent, monomer(s) and hydrogen in a flash separation stage.
  • the liquid medium of the first stage does not disturb the gas phase reaction.
  • the transfer of polymer powder may be difficult in some cases.
  • the polymer powder should contain only a small fraction of polymer particles having a small diameter. These small particles are often referred to as fines. If the fines are present in a high amount, so that more than about 15% of the particles have a diameter smaller than 100 microns, problems in the operation of the gas phase reactor and/or product transfer are likely. It has been found that the fines are present already after the first polymerization stage. Different methods to reduce the level of fines have been presented, like the use of a prepolymerization reactor, as disclosed in WO-A- 96/18662 (based on FI-A-945926).
  • the polymer is prepared in the first stage in the presence of a first liquid medium comprising diluent with monomer(s) and possibly hydrogen dissolved therein.
  • the polymer is separated from the first liquid medium and mixed in a second liquid medium. This is suitably done in a washing apparatus. After the separation, the polymer powder is then transferred with a third liquid medium into the gas phase reactor. Thus no dry polymer powder needs to be transferred.
  • the second liquid medium may be the same as or different from the diluent used in the first polymerization stage.
  • the second and third liquid mediums have such boiling point and vapor pressure that they evaporate in the conditions employed in the second polymerization stage in the gas phase reactor.
  • the third liquid medium is most preferably obtained by condensing a part of the recycle gas of the gas phase reactor. It has been found that in a process where the first polymerization stage is conducted in a slurry reactor and the second polymerization stage in a gas phase reactor and the hydrocarbons are separated from the polymer after the slurry reactor by flashing, the fines are mainly produced at the flash stage. The particles break when the pressure is reduced and the hydrocarbons are released from the particles. In accordance with the invention, the formation of polymer fines is minimized, when there is no flash stage.
  • the invention can be used especially in the polymerization or copolymerization of olefins, such as ethylene or propylene or their mixture, optionally together with higher alpha-olefins.
  • olefins such as ethylene or propylene or their mixture
  • the first stage is preferably carried out in a loop reactor, and the second stage in a fluidized bed reactor.
  • Figure 1 is a schematic representation of a two-stage polymerization process.
  • the first polymerization stage is a slurry polymerization, and it is preferably carried out in a loop reactor.
  • a suitable inert low-boiling hydrocarbon can be used as a reaction medium.
  • hydrocarbons propane, butane, and pentane.
  • higher hydrocarbons such as hexane, heptane, octane, cyclo- hexane, or cycloheptane, can be used.
  • special advantages can be achieved, if the liquid medium is in supercritical state, i.e. the temperature in the reactor exceeds the critical temperature of the fluid mixture and the pressure in the reactor exceeds the critical pressure of the fluid mixture.
  • propane can be used as a diluent in supercritical operating conditions.
  • bimodal polyethylene When e.g. bimodal polyethylene is produced, it is common to produce the low molecular weight component in the slurry stage. Hydrogen is used to control the molecular weight. To produce the low molecular weight component, a relatively high hydrogen concentration is needed. Thus, the hydrogen to ethylene molar ratio in the slurry reactor is typically between 200-800 mol/kmol, depending on the requirements of the product to be produced. It is also possible to produce the high molecular weight component in the first stage. This is usually the case for instance when bimodal polypropylene is produced. In this case hydrogen is not necessarily present in the first stage.
  • the second polymerization stage in accordance with the invention is conducted in a gas phase.
  • the second polymerization stage is conducted in a gas fluidized bed reactor.
  • a gas fluidized bed reactor comprises a gas inlet at the bottom of the reactor, a gas distributor plate above the gas inlet, a bed of polymer particles above the gas distributor plate, and a gas outlet at the top of the reactor. It also comprises an inlet for polymer particles from the previous polymerization stage and an outlet for removing the polymer product. Moreover, it may comprise an agitator to assist in keeping the bed in a thoroughly mixed state.
  • the gas is introduced into the bottom of the reactor.
  • the gas distributor plate distributes the upwardly flowing gas uniformly into the bed.
  • the velocity of the gas needs to be such that it supports the particles forming the bed and maintains the bed in fluidized state.
  • the unreacted gas is collected from the top of the reactor, compressed and cooled.
  • the compressed and cooled gas is reintroduced into the bottom of the reactor.
  • the recycle gas may be cooled to such an extent that part of it is condensed, as disclosed in EP-B-89691 or EP-B-699213.
  • the condensed liquid may then be introduced into the bed as a two-phase stream containing gas and liquid, as disclosed in EP-B-89691, or the liquid may be separated from the gas stream and introduced as a separate liquid stream into the reactor, as disclosed in EP-B-699213.
  • the high molecular weight component is usually produced in the gas phase reactor. Then, relatively low concentrations of hydrogen are needed. Depending on the requirements of the final product, the required hydrogen to ethylene molar ratio may be as low as 5 mol kmol. When products having a lower viscosity are produced, the hydrogen to ethylene ratio may be about 100 mol/kmol.
  • Said polymer slurry is then preferably led into a suitable separation apparatus, preferably on the top of a washing apparatus.
  • a suitable second liquid medium is introduced into the bottom of the apparatus.
  • the solid polymer moves downwards to the bottom, and the liquid moves countercurrently upwards.
  • a stream consisting mainly of liquid together with reactants and polymer dissolved therein is collected from the top of the apparatus and a stream consisting mainly of concentrated polymer slurry is collected from the bottom of the apparatus.
  • the volume of the second liquid medium must be at least 0.5 times the volume of the slurry from the first polymerization stage, and preferably at least the volume of the slurry from the first polymerization stage. This means that the volume of the second liquid medium introduced into the bottom of the washing apparatus must be at least as high as the volume of the liquid taken out with the polymer from the bottom of the apparatus.
  • the concentrated polymer slurry is mixed with a suitable third liquid medium, and the mixture is transferred into the gas phase reactor.
  • the first liquid medium of the first polymerization stage together with a part of the second liquid medium is removed from the top of the apparatus.
  • the liquid collected from the top of the washing apparatus is preferably recycled into the first polymerization stage.
  • washing or extraction apparatus e.g. such a plain wash column as has been suggested in US-A-4121029 to be used in a pipeloop reactor system for recovery of soluble catalysts components from polymer slurry effluent.
  • This column has a settling leg, into which the particles settle because of their higher density.
  • the second liquid medium is preferably fed into the bottom of the column at a rate which is essentially lower than the settling rate of the particles.
  • a column provided with a mixing apparatus can also be used, especially if it can be expected that the polymer will attach to the walls of the column.
  • the process according to the invention has also a benefit of avoiding the carry-over of the reactants from the first polymerization stage into the second polymerization stage.
  • the liquid medium forming the slurry in which the polymer is introduced into the gas phase reactor preferably evaporates in that reactor, thus cooling the reactor. Such cooling is effective and leads to a well controlled temperature throughout the reactor.
  • the first liquid medium comprises the diluent used in the slurry polymerization, together with monomer, eventual comonomers and optionally hydrogen dissolved therein.
  • the second liquid medium introduced into the bottom of the washing apparatus is preferably pure diluent used in the slurry polymerization stage, possibly containing traces of monomer(s) and hydrogen.
  • the third liquid medium which is used to assist the transfer of the slurry into the gas phase reactor is preferably a condensate which has been obtained by condensing a part of the recycle gas flow of the gas phase reactor.
  • the temperature and pressure in the washing apparatus are selected so that the fluid within the apparatus remains as liquid.
  • the temperature is preferably lower than the operating temperature of the gas phase reactor, that is usually lower than 80 °C.
  • the lower limit may be chosen based on economical considerations.
  • a suitable range of temperature of the washing apparatus is between 40 °C and 80 °C.
  • the operating pressure of the washing apparatus should be lower than the operating pressure of the slurry reactor but higher than the operating pressure of the gas phase reactor. Moreover, the operating pressure should be selected so that no significant flashing occurs in the slurry reactor discharge line.
  • a suitable range of operating pressure is from about 5 to 25 bar lower than the operating pressure in the slurry polymerization stage, or from 30 to 55 bar.
  • Some undesired components such as waxes, are also formed in the first stage. Such soluble components do not accumulate in the washing apparatus but are removed together with the first stage liquid medium.
  • the waxy components are preferably removed by evaporation. Less reacted fine particles from the first stage are also removed with the first stage liquid medium from the separation apparatus. This is also advantageous since such fine particles may cause inhomogeneity in the powder of the gas phase reactor. Such particles can also be removed so as to not enrich in the slurry reactor.
  • the polymerization stages are preferably carried out according to the description in WO-A-92/12182 (corresponds to FI-A-906428), WO-A-96/18662 (corresponds to FI-A-945926), WO-A-96/18662 (corresponds to FI-B-96216), or EP-A-688794 (corresponds to FI-A-942949).
  • the enclosed drawing describes two-stage processes for preparing polyethylene.
  • Figure 1 describes one preferred embodiment of the invention.
  • Ethylene, hydrocarbon medium (propane), hydrogen, and optionally comonomer are fed through a line 1 into a loop reactor 2.
  • Solid catalyst (and possible cocatalyst) is fed through a separate line 3.
  • the reaction mixture is circulated by suitable means.
  • the reactor is suitably cooled.
  • the reactor can be also otherwise controlled. E.g., the reaction mixture can be analyzed, and the amount of the possible cocatalyst can be adjusted.
  • the reaction mixture is fed through a line 4 on the top of an extraction column 5 provided with a mixer.
  • the solid polymer containing the catalyst moves downwards to the bottom.
  • Dispersion medium is fed through a line 6 on the bottom of the column, and the polymer is further transferred with the dispersing medium through a line 7 into a fluidized bed reactor 8.
  • the dispersion medium evaporates in the reactor.
  • Ethylene, and possible other components, such as comonomer, nitrogen, and hydrogen, are fed into the reactor through a line 9.
  • the polymer particles form a bed on the gas distribution plate of the reactor. The bed is maintained in a fluidized state by introducing an upwardly flowing gas flow from the bottom of the reactor through the gas distribution plate.
  • Unreacted gas is taken from the top of the reactor through a line 10.
  • the gas is cooled in a cooler 11 so that part of it condenses.
  • the partially condensed gas flow is further led into a tank 12.
  • the noncondensed part of the gas flow is fed from the a tank 12 through a line 13 to the bottom of the reactor.
  • the condensed part of the gas flow is led from the tank 12 via a conduit 6 to the bottom of the extraction column 5 to be used as the dispersion medium.
  • Polymer is removed from the gas phase reactor 8 through a line 14.
  • the hydrocarbon medium is removed from the top of the extraction column 5 through a line 15. Waxes are removed as dissolved in the hydrocarbon. Also finest particles are removed together with the hydrocarbon flow.
  • the hydrocarbon may be separated from the waxes in an evaporator 16, and most of the hydrocarbon is recycled through a line 17 into the loop reactor 3. Part of the hydrocarbon is fed through a hydrogen separator 18 and line 19 as a wash liquid above the dispersion medium into the extraction column. It is preferable that the mixing of the wash liquid and the dispersion medium is avoided as far as possible.
  • reaction medium of the loop reactor may be mixed with the condensate led to the bottom.
  • the amount can be kept so slow that it has in practice no effect in the gas phase reactor.
  • some condensate may be mixed with the liquid removed from the top of the column, but also this amount can be kept so slow as to not have any effect.
  • the top of the column 5 may have the shape of a hydrocyclone to enhance the separation.
  • a cocatalyst is used in the loop reactor, and this cocatalyst is separated from the polymer together with the reaction medium. Different cocatalyst can then be used in the gas phase reactor. In a typical arrangement, about 1/30 - 1/5 of the cocatalyst used in the slurry reactor can be removed.
  • the second liquid medium is introduced into the middle zone of the column 25.
  • the introduction of the liquid into the middle zone divides the column into two zones. In the upper zone there is an upward liquid flow and in the lower zone there is a downward liquid flow.
  • the upwardly flowing liquid which contains the major fraction of the first liquid medium comprising the diluent, ethylene and hydrogen from the loop reactor, is collected from the top of the column via conduit 15.
  • the downwardly flowing liquid which contains the major fraction of the third liquid medium comprising the condensed part of the recycle gas stream, is collected from the bottom of the column via the conduit 7.
  • Examples 4 to 6 show the influence of flashing especially on the particle size distribution.
  • MFR was measured accorning to ISO 1133, at 190 °C.
  • Particle size distribution was determined by laser diffraction method, using an equipment by Malvern. The fines were considered as particles having a diameter smaller than 100 microns.
  • the slurry is then introduced into the top of an extraction column operating at 45 °C, where it is flushed with a fresh diluent fed from the bottom of the column.
  • the volumetric flow rate of slurry at this temperature is 24 m 3 /h.
  • the density of the fluid phase is 520 kg/m 3 .
  • the volumetric flow rate of the fresh wash diluent is 0.5 times the volumetric flow rate of slurry, i.e. 12 m /h.
  • the diameter of the extraction column is 1.5 m and the length is 6 m.
  • Example 1 The process according to the Example 1 is operated in otherwise similar manner, except that the ratio r of volumetric feed flow of wash diluent to the volumetric flow of polymer slurry is 1.0 instead of 0.5. The results are shown in Table 1.
  • Example 1 The process according to the Example 1 is operated in otherwise similar manner, except that the ratio r of volumetric feed flow of wash diluent to the volumetric flow of polymer slurry is 0.75 instead of 0.5. The results are shown in Table 1.
  • Ethylene was continuously polymerized at a rate of 25 kg/h in a 500 dm loop reactor operating at 95 °C temperature and 60 bar pressure in the presence of a catalyst prepared according to Example 3 of EP-688794.
  • the slurry containing the liquid medium and the polymer were discharged intermittently from the reactor to a flash tank operating at 3 bar pressure.
  • the composition of the liquid medium was analyzed and it was found to contain about 88% by mole propane, 7% by mole ethylene and 3% by mole hydrogen.
  • the remaining 2% contained aliphatic hydrocarbons, like methane, ethane, n-butane and isobutane.
  • a polymer sample was taken from the flash tank. The particle size distribution was measured. It was found that the fraction of particles having a diameter less than 100 microns was about 15%.
  • Ethylene was continuously polymerized as in Example 4.
  • the slurry containing the liquid medium and the polymer were discharged intermittently from the reactor without a flashing stage directly to the gas phase reactor.
  • the composition of the liquid medium was analyzed and it was found to contain about 88% by mole propane, 7% by mole ethylene and 3% by mole hydrogen.
  • the remaining 2% contained aliphatic hydrocarbons, like methane, ethane, n-butane and isobutane.
  • a polymer sample was taken from the slurry into a 3 dm 3 stainless steel sample container having valves at both ends.
  • the liquid medium was slowly removed from the sample by evaporating the medium during a period of 30 minutes by carefully opening one of the valves.
  • the particle size distribution of the polymer was measured. It was found that the fraction of particles having a diameter less than 100 microns was about 6%. Thus, this example shows that the level of fines can be significantly reduced if the flashing stage can be avoided.
  • the polymerization in the loop reactor was done according to Example 4.

Abstract

Cette invention a trait à un procédé de transfert d'un matériau polymère d'un réacteur à combustible en suspension dans un réacteur à phase gazeuse. Le matériau polymère en suspension dans le réacteur à combustible en suspension est séparé, mélangé à un deuxième milieu liquide, puis à un troisième et, ensuite, transféré avec ce dernier dans le réacteur à phase gazeuse.
PCT/FI2000/000032 1999-01-18 2000-01-18 Procede de transfert d'un materiau polymere dans un reacteur a phase gazeuse WO2000042077A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU22961/00A AU2296100A (en) 1999-01-18 2000-01-18 Method for transferring polymer into a gas phase reactor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI990081A FI990081A0 (fi) 1999-01-18 1999-01-18 Menetelmä polymeerin siirtämiseksi kaasufaasireaktoriin
FI990081 1999-01-18

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WO2000042077A1 true WO2000042077A1 (fr) 2000-07-20

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002026841A1 (fr) * 2000-09-26 2002-04-04 Basell Poliolefine Italia S.P.A. Procede de preactivation de catalyseurs
EP1415999A1 (fr) * 2002-10-30 2004-05-06 Borealis Technology Oy Procédé et dispositif pour la production de polymères d' oléfines
EP2330135A1 (fr) 2009-12-02 2011-06-08 Borealis AG Procédé de production de polyoléfines
US9139673B2 (en) 2012-03-16 2015-09-22 Ineos Europe Ag Process for introduction of liquid feeds to a polymerization process
JP2016535662A (ja) * 2013-09-25 2016-11-17 ティコナ・エルエルシー 複数の化合物からポリマーを分離するための方法及びシステム
US9540467B2 (en) 2013-08-14 2017-01-10 Ineos Europe Ag Polymerization process
EP3135694A1 (fr) * 2015-08-27 2017-03-01 SABIC Global Technologies B.V. Procede de polymerisation en continu de monomeres d'olefines dans un reacteur
WO2020172387A1 (fr) 2019-02-20 2020-08-27 Fina Technology, Inc. Polypropylène à stabilité thermique améliorée

Citations (3)

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Publication number Priority date Publication date Assignee Title
US4692501A (en) * 1982-02-06 1987-09-08 Mitsui Petrochemical Industries, Ltd. Process for continuous multi-stage polymerization of olefins
US5175208A (en) * 1988-07-18 1992-12-29 Mitsui Toatsu Chemicals, Inc. Method for preparing block copolymers of propylene
WO1998059002A1 (fr) * 1997-06-24 1998-12-30 Borealis A/S Copolymere de propylene heterophase et son procede de preparation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4692501A (en) * 1982-02-06 1987-09-08 Mitsui Petrochemical Industries, Ltd. Process for continuous multi-stage polymerization of olefins
US5175208A (en) * 1988-07-18 1992-12-29 Mitsui Toatsu Chemicals, Inc. Method for preparing block copolymers of propylene
WO1998059002A1 (fr) * 1997-06-24 1998-12-30 Borealis A/S Copolymere de propylene heterophase et son procede de preparation

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002026841A1 (fr) * 2000-09-26 2002-04-04 Basell Poliolefine Italia S.P.A. Procede de preactivation de catalyseurs
EP1415999A1 (fr) * 2002-10-30 2004-05-06 Borealis Technology Oy Procédé et dispositif pour la production de polymères d' oléfines
WO2004039847A1 (fr) * 2002-10-30 2004-05-13 Borealis Technology Oy Procede et appareil de production de polymeres d'olefines
JP2006504821A (ja) * 2002-10-30 2006-02-09 ボレアリス テクノロジー オイ オレフィン重合体を製造する方法および装置
US7115687B2 (en) 2002-10-30 2006-10-03 Borealis Technology Oy Process and apparatus for producing olefin polymers
EP2330135A1 (fr) 2009-12-02 2011-06-08 Borealis AG Procédé de production de polyoléfines
WO2011066892A1 (fr) 2009-12-02 2011-06-09 Borealis Ag Procédé de fabrication de polyoléfines
US8476383B2 (en) 2009-12-02 2013-07-02 Borealis Ag Process for producing polyolefins
US9328183B2 (en) 2012-03-16 2016-05-03 Ineos Europe Ag Polymerization process
US9175120B2 (en) 2012-03-16 2015-11-03 Ineos Europe Ag Polymerisation process
US9139673B2 (en) 2012-03-16 2015-09-22 Ineos Europe Ag Process for introduction of liquid feeds to a polymerization process
US9567411B2 (en) 2012-03-16 2017-02-14 Ineos Europe Ag Polymerisation process
US9605091B2 (en) 2012-03-16 2017-03-28 Ineos Europe Ag Separation of monomer components from light components
US9540467B2 (en) 2013-08-14 2017-01-10 Ineos Europe Ag Polymerization process
JP2016535662A (ja) * 2013-09-25 2016-11-17 ティコナ・エルエルシー 複数の化合物からポリマーを分離するための方法及びシステム
EP3135694A1 (fr) * 2015-08-27 2017-03-01 SABIC Global Technologies B.V. Procede de polymerisation en continu de monomeres d'olefines dans un reacteur
WO2017032682A1 (fr) * 2015-08-27 2017-03-02 Sabic Global Technologies B.V. Procédé pour la polymérisation en continu de monomères oléfiniques dans un réacteur
US10822435B2 (en) 2015-08-27 2020-11-03 Sabic Global Technologies B.V. Process for continuous polymerization of olefin monomers in a reactor
WO2020172387A1 (fr) 2019-02-20 2020-08-27 Fina Technology, Inc. Polypropylène à stabilité thermique améliorée
US11780939B2 (en) 2019-02-20 2023-10-10 Fina Technology, Inc. Enhanced heat stability polypropylene

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