EP1079916A1 - Reacteur a lit fluidise en phase gazeuse - Google Patents

Reacteur a lit fluidise en phase gazeuse

Info

Publication number
EP1079916A1
EP1079916A1 EP99922161A EP99922161A EP1079916A1 EP 1079916 A1 EP1079916 A1 EP 1079916A1 EP 99922161 A EP99922161 A EP 99922161A EP 99922161 A EP99922161 A EP 99922161A EP 1079916 A1 EP1079916 A1 EP 1079916A1
Authority
EP
European Patent Office
Prior art keywords
gas
fluidized bed
reactor
phase fluidized
bed reactor
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP99922161A
Other languages
German (de)
English (en)
Inventor
Rainer Karer
Kaspar Evertz
Wolfgang Micklitz
Hans-Jacob Feindt
Philipp Rosendorfer
Peter KÖLLE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Basell Polyolefine GmbH
Original Assignee
Basell Polyolefine GmbH
Elenac GmbH
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
Priority claimed from DE1998121955 external-priority patent/DE19821955A1/de
Priority claimed from DE1999104811 external-priority patent/DE19904811A1/de
Application filed by Basell Polyolefine GmbH, Elenac GmbH filed Critical Basell Polyolefine GmbH
Publication of EP1079916A1 publication Critical patent/EP1079916A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • 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
    • B01J8/44—Fluidisation grids
    • 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
    • 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
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
    • 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

Definitions

  • the present invention relates to a gas phase fluidized bed reactor for the polymerization of ethylenically unsaturated monomers.
  • a reactor chamber (1) in the form of a vertical tube, if desired a calming zone (2) adjoining the upper part of the reactor chamber, a circulating gas line (3), a circulating gas compressor (4) and a cooling device (5), characterized in that in the area of the transfer of the reaction gas from the circulating gas line into the reactor space and in the lower part of the reactor space itself there is either no gas distributor plate at all or only a gas distributor plate whose total area of the gas passage openings is more than 20% of the total area of this gas distributor plate.
  • the schematic structure of the reactor is shown in Figure 1.
  • the invention relates to processes for the polymerization of ethylene or copolymerization of ethylene with C 3 - to Cs-Ct olefins and for the production of EPDM, which are carried out in such a reactor.
  • Gas phase polymerization processes are among the preferred processes for the polymerization of ethylenically unsaturated monomers, in particular for the polymerization of ethylene, if desired in the presence of further unsaturated monomers. Polymerization processes in fluidized beds are particularly economical.
  • Gas phase fluidized bed reactors for carrying out such processes have long been known.
  • the reactors common today have many common structural features: Among other things, they consist of a reactor space in the form of a vertical tube, which usually has an enlarged diameter in the upper part. In this calming zone there is a smaller gas flow due to the larger pipe diameter, which leads to a limitation of the discharge of the fluidized bed consisting of small polymer.
  • these reactors contain a circulating gas line, in which cooling units for removing the heat of polymerization, a compressor and, if desired, further elements such as a cyclone for removing fine polymer particles are attached.
  • a reactor floor in the usual form today i.e. a close-meshed network or a metal plate with narrow bores of different geometries, has some disadvantages: Both on the inflow side of the floor and on the top of the floor, polymer deposits caused by dust can occur again and again. shaped polymer and catalyst particles, which are entrained by the gas flow into the circulating gas line. This danger is particularly prevalent in the so-called condensed mode mode, i.e. when liquid monomers are present in the cycle gas. In addition to these deposits, which can lead to an increase in pressure and ultimately to a termination of the polymerization, the pressure loss in normal operation also causes additional energy costs, since the compressor has to compensate for this pressure loss by higher output.
  • the object of the present invention was therefore to provide a gas phase fluidized bed reactor which no longer has these disadvantages.
  • the gas phase fluidized bed reactor according to the invention is suitable in principle for the polymerization of various ethylenically unsaturated monomers.
  • ethylenically unsaturated monomers examples include ethylene, propylene, 1-butene, isobutene, 1-pentene, 1-hexene, 1-heptene, 1-octene and also higher ⁇ -olefins; dienes such as butadiene and cyclopentadiene and cycloolefins such as cyclopentene and cyclohexene are also suitable.
  • the ethylenically unsaturated monomers can be polymerized alone or as a mixture.
  • the reactor according to the invention is particularly suitable for the homopolymerization of ethylene, for the production of ethylene-hexene and ethylene-butene copolymers and for the production of EPDM.
  • a preferred embodiment of the gas phase fluidized bed reactor according to the invention is characterized in that there is no gas distributor floor itself in the area of the transfer of the reaction gas from the circulating gas line into the reactor space and in the lower part of the reactor space itself.
  • a reactor in which in the area of the reaction gas transfer from the circulating gas line into the reactor space or in the lower part of the reaction space itself a gas distributor plate, the total area of the gas passage openings of which is more than 50%, particularly preferably more than 90%, of the total surface area of this gas distributor plate , is available.
  • flow transducers should be installed, particularly in the case of large reactor dimensions, when the circulating gas is transferred from the circulating gas line to the reaction space in order to convert the flow pulse of the incoming gas.
  • This can be done by various gas deflecting devices such as baffles, deflectors, impact plates or the like, as are known to the person skilled in the art.
  • gas phase fluidized bed reactors in which flow baffles are arranged in the area of the reaction gas transfer from the circulating gas line into the reactor space for converting the flow impulse of the incoming gas, which are arranged in such a way that a largely homogeneous introduction of the gas flow into the fluidized bed is achieved.
  • sheet metal is of course not intended to describe the material of the device, but only its shape and function; the kind of
  • Another preferred device for gas distribution when entering the reaction space of the reactor according to the invention consists in that in the area of the reaction gas transfer from the circulating gas line into the reactor space for converting the flow impulse of the entering gas, a coarse-meshed network is attached, on which balls are fixed in such number, size and distribution that a largely homogeneous introduction of the gas flow into the fluidized bed is achieved.
  • the net should be so coarse-meshed that there is practically no pressure loss;
  • the task of this network is to keep the balls, which act as deflectors or deflectors for the gas flow, in the desired position.
  • the balls can be evenly distributed over the network. In the case of a large reactor diameter in particular, however, it can make sense to that is, directly above the gas influence in the middle of the reactor section, to arrange a larger number of such balls than in the edge area.
  • the gas phase fluidized bed reactors according to the invention show their advantageous properties, especially on an industrial scale.
  • Reactors are preferred in which the inner diameter of the reaction space (1) is more than 0.5 m, particularly preferably more than 1 m.
  • Reactors with internal diameters between 2 and 8 m are particularly advantageous.
  • the reactor according to the invention can be provided with various devices for gas / solid separation.
  • a calming zone (2) adjoins the upper part of the reactor space (1).
  • Another embodiment of the gas phase fluidized bed reactor according to the invention is characterized in that a cyclone for separating polymer and catalyst particles from the circulating gas is attached between the reactor space (1) and the aggregates of the circulating gas line. If desired, this cyclone can also be combined with a calming zone (2).
  • this calming zone is dispensed with, so that the circulating gas line or, in addition, a device for separating polymer and catalyst particles from the circulating gas, for example a cyclone, is connected directly to the reactor space.
  • a device for separating polymer and catalyst particles from the circulating gas for example a cyclone
  • the reactors according to the invention have no reactor base which can prevent the polymer particles from flowing back into the circulating gas line when the compressor is switched off, it may be expedient to take measures to prevent this backfeeding.
  • a flap or a slide in the area of the mouth of the circulating gas line can be attached to the reaction space. B. can also be closed when filling the reactor before the start of the polymerization, but when starting the compressor is opened.
  • a preferred embodiment of the invention provides that the closable flap or the slide is provided with uniformly distributed holes, which preferably have a diameter between 1 and 7 mm. With the help of this flap, the bulk material can be whirled up when the flap is initially closed.
  • the gas phase fluidized bed reactor described here is particularly suitable for carrying out processes for the polymerization of ethylene or for the copolymerization of ethylene with C 3 - to Cs-.alpha.-olefins, as mentioned at the outset.
  • a process for the production of EPDM is preferred, which is characterized in that the copolymerization is carried out in a reactor according to the invention.
  • an advantageous embodiment of the process according to the invention consists in feeding a mixture containing gaseous and liquid monomers into the reactor space.
  • the polymerization process according to the invention is carried out in such a way that the polymerization takes place essentially in the reactor space (1) and only small amounts of particles circulate with the circulating gas. This can be achieved by the above-mentioned devices for gas-solid separation. Often, however, such devices can largely be described if the polymerization is carried out only just below the softening temperature of the polymers.
  • a copolymerization was carried out in this reactor under the following conditions:
  • the polymerization was carried out continuously for 60 hours. After the polymerization, the reactor was opened, there were kei ⁇ nerlei chunks or coverings visible.

Abstract

L'invention concerne un réacteur à lit fluidisé en phase gazeuse pour la polymérisation de monomères éthyléniquement insaturés, comportant une chambre de réacteur (1) se présentant sous forme d'un tube vertical, éventuellement une zone de stabilisation (2) se raccordant à la partie supérieure de la chambre de réacteur, une canalisation de gaz circulaire (3), un compresseur à gaz circulaire (4) et un système de refroidissement (5). Dans la région de transfert du gaz de réaction de la canalisation de gaz circulaire à la chambre de réacteur, et dans la partie inférieure de la chambre de réacteur elle-même, on ne trouve généralement aucun distributeur de gaz ou bien alors un seul distributeur de gaz, la surface totale des orifices de passage de gaz de celui-ci atteignant plus de 20 % de la surface totale de ce distributeur de gaz.
EP99922161A 1998-05-15 1999-05-04 Reacteur a lit fluidise en phase gazeuse Withdrawn EP1079916A1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE19821955 1998-05-15
DE1998121955 DE19821955A1 (de) 1998-05-15 1998-05-15 Gasphasenwirbelschichtreaktor
DE1999104811 DE19904811A1 (de) 1999-02-05 1999-02-05 Gasphasenwirbelschichtreaktor
DE19904811 1999-02-05
PCT/EP1999/003007 WO1999059712A1 (fr) 1998-05-15 1999-05-04 Reacteur a lit fluidise en phase gazeuse

Publications (1)

Publication Number Publication Date
EP1079916A1 true EP1079916A1 (fr) 2001-03-07

Family

ID=26046231

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99922161A Withdrawn EP1079916A1 (fr) 1998-05-15 1999-05-04 Reacteur a lit fluidise en phase gazeuse

Country Status (7)

Country Link
US (2) US7601303B1 (fr)
EP (1) EP1079916A1 (fr)
JP (1) JP2002515516A (fr)
KR (1) KR100632907B1 (fr)
CN (1) CN1191114C (fr)
CA (1) CA2332269C (fr)
WO (1) WO1999059712A1 (fr)

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CN100435928C (zh) * 2006-09-20 2008-11-26 浙江大学 一种气体分布器
JP5308794B2 (ja) 2007-12-11 2013-10-09 住友化学株式会社 噴流層装置を用いたポリオレフィン製造方法
JP5427396B2 (ja) 2007-12-11 2014-02-26 住友化学株式会社 粉体移送装置、及び、ポリオレフィンの製造方法
JP5249730B2 (ja) 2007-12-11 2013-07-31 住友化学株式会社 オレフィン重合反応装置及びポリオレフィン製造方法
JP5308797B2 (ja) 2007-12-11 2013-10-09 住友化学株式会社 オレフィン重合反応装置、ポリオレフィン製造システム、及び、ポリオレフィン製造方法
JP5308795B2 (ja) * 2007-12-11 2013-10-09 住友化学株式会社 ポリオレフィン製造方法、並びに、噴流層装置を備えたポリオレフィン製造システム
US20090163756A1 (en) * 2007-12-19 2009-06-25 Uop Llc, A Corporation Of The State Of Delaware Reactor cooler
US8129482B2 (en) * 2008-02-27 2012-03-06 Westlake Longview Corporation Method of preventing or reducing polymer agglomeration on grid in fluidized-bed reactors
JP5545800B2 (ja) 2009-06-08 2014-07-09 住友化学株式会社 噴流−流動層型オレフィン重合反応装置、ポリオレフィン製造システム、及び、ポリオレフィン製造方法
WO2012061742A1 (fr) 2010-11-05 2012-05-10 ThermoChem Recovery International Système de circulation de solides et méthode de capture et de conversion de solides réactifs
EP2465877A1 (fr) 2010-12-20 2012-06-20 Ineos Commercial Services UK Limited Procédé
ES2813282T3 (es) * 2011-03-02 2021-03-23 Borealis Ag Conjunto de reactor de alto rendimiento para la polimerización de olefinas
HUE052511T2 (hu) * 2011-03-02 2021-05-28 Borealis Ag Eljárás polimerek elõállítására
CN105584991B (zh) 2011-09-27 2019-05-14 国际热化学恢复股份有限公司 合成气净化系统和方法
CN103446961A (zh) * 2013-09-22 2013-12-18 刘东升 一种颗粒流化设备
CN104888984A (zh) * 2014-03-05 2015-09-09 中国石化工程建设有限公司 一种磁旋流分离器及分离装置和方法
CN104558330B (zh) * 2014-12-31 2017-07-21 浙江大学 一种气相聚合制备多层核壳结构聚合物粒子的方法
CA2891002C (fr) * 2015-05-13 2022-09-06 Veronica Rose Zimmerman Modelisation d'une plaque de lit et de son utilisation
EP3184166A1 (fr) * 2015-12-22 2017-06-28 Borealis AG Procédé pour retirer des agglomérats à partir d'un réacteur à lit fluidisé
CA3014874C (fr) 2016-02-16 2019-03-19 Thermochem Recovery International, Inc. Systeme et procede de generation de produit gazeux integre en energie a deux etages
CN109153929B (zh) 2016-03-25 2019-12-20 国际热化学恢复股份有限公司 三阶段能量集成产物气体发生系统和方法
JP6902337B2 (ja) 2016-08-03 2021-07-14 住友化学株式会社 ヘテロファジックプロピレン重合材料の製造方法
US10364398B2 (en) 2016-08-30 2019-07-30 Thermochem Recovery International, Inc. Method of producing product gas from multiple carbonaceous feedstock streams mixed with a reduced-pressure mixing gas
US10099200B1 (en) 2017-10-24 2018-10-16 Thermochem Recovery International, Inc. Liquid fuel production system having parallel product gas generation
JP7297056B2 (ja) * 2018-09-06 2023-06-23 パブリック・ジョイント・ストック・カンパニー・“シブール・ホールディング” バブルシェルアンドチューブ装置
CN111659322A (zh) * 2019-03-06 2020-09-15 浙江佳汇新材料有限公司 一种制备1,1,1,3-四氯丙烷的装置及工艺
US11555157B2 (en) 2020-03-10 2023-01-17 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas
US11466223B2 (en) 2020-09-04 2022-10-11 Thermochem Recovery International, Inc. Two-stage syngas production with separate char and product gas inputs into the second stage

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Also Published As

Publication number Publication date
KR100632907B1 (ko) 2006-10-16
WO1999059712A1 (fr) 1999-11-25
CN1301192A (zh) 2001-06-27
US7601303B1 (en) 2009-10-13
KR20010043631A (ko) 2001-05-25
CA2332269C (fr) 2008-01-22
JP2002515516A (ja) 2002-05-28
US20100056734A1 (en) 2010-03-04
CA2332269A1 (fr) 1999-11-25
US8034884B2 (en) 2011-10-11
CN1191114C (zh) 2005-03-02

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