EP1079916A1 - Gasphasenwirbelschichtreaktor - Google Patents
GasphasenwirbelschichtreaktorInfo
- 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- Withdrawn
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
Description
Claims
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 (de) | 1998-05-15 | 1999-05-04 | Gasphasenwirbelschichtreaktor |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1079916A1 true EP1079916A1 (de) | 2001-03-07 |
Family
ID=26046231
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99922161A Withdrawn EP1079916A1 (de) | 1998-05-15 | 1999-05-04 | Gasphasenwirbelschichtreaktor |
Country Status (7)
Country | Link |
---|---|
US (2) | US7601303B1 (de) |
EP (1) | EP1079916A1 (de) |
JP (1) | JP2002515516A (de) |
KR (1) | KR100632907B1 (de) |
CN (1) | CN1191114C (de) |
CA (1) | CA2332269C (de) |
WO (1) | WO1999059712A1 (de) |
Families Citing this family (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 (en) | 2010-11-05 | 2012-05-10 | ThermoChem Recovery International | Solids circulation system and method for capture and conversion of reactive solids |
EP2465877A1 (de) | 2010-12-20 | 2012-06-20 | Ineos Commercial Services UK Limited | Verfahren |
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 (en) * | 2015-05-13 | 2022-09-06 | Veronica Rose Zimmerman | Modeling a bed plate and its use |
EP3184166A1 (de) * | 2015-12-22 | 2017-06-28 | Borealis AG | Verfahren zum entnehmen von agglomeraten aus einem fliessbettreaktor |
CA3014874C (en) | 2016-02-16 | 2019-03-19 | Thermochem Recovery International, Inc. | Two-stage energy-integrated product gas generation system and method |
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 |
Family Cites Families (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2636712A (en) * | 1950-04-03 | 1953-04-28 | Standard Oil Dev Co | Slide valve for regulating the flow of solids |
NL137126C (de) | 1961-09-28 | |||
US3829983A (en) * | 1971-10-27 | 1974-08-20 | Phillips Petroleum Co | Grid plate |
US4323312A (en) * | 1977-08-26 | 1982-04-06 | Werner Glatt | Fluidized bed apparatus |
EP0047794B1 (de) | 1980-09-15 | 1983-07-06 | Saat- und Erntetechnik GmbH. | Verfahren zur gleichmässigen, geschlossenen Oberflächenbeschichtung einzelner Körner von rieselfähigen Gütern und Vorrichtung zu seiner Durchführung |
DE3227932A1 (de) | 1982-07-27 | 1984-02-02 | Basf Ag, 6700 Ludwigshafen | Vorrichtung zur umsetzung von gasen und gasen oder feststoffen zu temperaturempfindlichen feststoffen in der wirbelschicht |
EP0201770B1 (de) * | 1985-04-24 | 1992-07-01 | Pratt & Whitney Canada, Inc. | Turbinenmotor mit induziertem Vordrall am Kompressoreinlass |
FR2581564B1 (fr) | 1985-05-13 | 1993-05-07 | Bp Chimie Sa | Appareil a lit fluidise comportant une grille de fluidisation a plusieurs pentes |
FR2617411B1 (fr) | 1987-06-30 | 1989-11-17 | Bp Chimie Sa | Dispositif et procede d'alimentation en gaz d'un appareil a lit fluidise |
EP0549252A1 (de) | 1991-12-23 | 1993-06-30 | BP Chemicals Limited | Verfahren zur Gasphase-Polymerisation von Alpha-Olefinen in einem Wirbelbettreaktor |
DE4217171A1 (de) * | 1992-05-23 | 1993-11-25 | Basf Ag | Kontinuierliches Gasphasenwirbelschichtverfahren zur Herstellung von Ethylenhomopolymerisaten und -copolymerisaten |
US5453471B1 (en) | 1994-08-02 | 1999-02-09 | Carbide Chemicals & Plastics T | Gas phase polymerization process |
DE4443292A1 (de) | 1994-12-06 | 1996-06-13 | Metallgesellschaft Ag | Verteilereinrichtung für ein Fluid in einem Behälter |
IT1275573B (it) * | 1995-07-20 | 1997-08-07 | Spherilene Spa | Processo ed apparecchiatura per la pomimerizzazione in fase gas delle alfa-olefine |
EP0825204B1 (de) | 1996-08-13 | 2002-06-05 | BP Chemicals Limited | Polymerisationsverfahren |
US6113862A (en) * | 1997-04-23 | 2000-09-05 | Union Carbide Chemicals & Plastics Technology Corporation | Fluidized bed polymerization reactor with multiple fluidization grids |
-
1999
- 1999-05-04 KR KR1020007012798A patent/KR100632907B1/ko not_active IP Right Cessation
- 1999-05-04 JP JP2000549369A patent/JP2002515516A/ja active Pending
- 1999-05-04 CN CNB998062006A patent/CN1191114C/zh not_active Expired - Fee Related
- 1999-05-04 CA CA002332269A patent/CA2332269C/en not_active Expired - Fee Related
- 1999-05-04 EP EP99922161A patent/EP1079916A1/de not_active Withdrawn
- 1999-05-04 US US09/700,367 patent/US7601303B1/en not_active Expired - Fee Related
- 1999-05-04 WO PCT/EP1999/003007 patent/WO1999059712A1/de active IP Right Grant
-
2009
- 2009-09-07 US US12/554,964 patent/US8034884B2/en not_active Expired - Fee Related
Non-Patent Citations (1)
Title |
---|
See references of WO9959712A1 * |
Also Published As
Publication number | Publication date |
---|---|
KR100632907B1 (ko) | 2006-10-16 |
WO1999059712A1 (de) | 1999-11-25 |
CN1301192A (zh) | 2001-06-27 |
US7601303B1 (en) | 2009-10-13 |
KR20010043631A (ko) | 2001-05-25 |
CA2332269C (en) | 2008-01-22 |
JP2002515516A (ja) | 2002-05-28 |
US20100056734A1 (en) | 2010-03-04 |
CA2332269A1 (en) | 1999-11-25 |
US8034884B2 (en) | 2011-10-11 |
CN1191114C (zh) | 2005-03-02 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO1999059712A1 (de) | Gasphasenwirbelschichtreaktor | |
DE69916895T2 (de) | Verfahren und vorrichtung zur entladung eines polymerisationsreaktors | |
DE69832234T2 (de) | Verfahren zur Herstellung von Propylen Polymeren und schlagzäh modifizierten Polymeren | |
EP1027146B1 (de) | Gasphasenpolymerisation in einem kelchreaktor | |
DE602005000036T2 (de) | Katalysatoreinsatz bei der herstellung von bimodalem polyolefin | |
DE60314852T2 (de) | Zyklon zur zentrifugaltrennung eines gemisches aus gas und feststoffteilchen | |
EP0963786B1 (de) | Gasphasenwirbelschichtreaktor | |
DE19907021A1 (de) | Verfahren und Apparatur zur Gasphasenpolymerisation von alpha-Olefinen | |
DE112006001239T5 (de) | Gasphasen-Wirbelschichtreaktor, Mehrgefäß-Polymerisationsreaktor und Verfahren zur Olefinpolymerherstellung | |
EP1363727B1 (de) | Verfahren zum dosieren von katalysatoren | |
DE60028636T2 (de) | Verfahren zur mehrstufigen Gasphasenpolymerisation und dafür geeignete Vorrichtung | |
DE69909088T2 (de) | Nachbehandlungsverfahren von polymeren, hergestellt mit hilfe des gasphasenpolymerisationsverfahrens in gegenwart von inerten partikeln | |
DE3015089A1 (de) | Verfahren zum herstellen von homopolymerisaten oder copolymerisaten des propylens | |
DE602004006853T2 (de) | Diskontinuierliche zugabe eines katalysators oder von zusatzstoffen in einen gasphasenfliessbettreaktor | |
DE3832082A1 (de) | Verfahren zum herstellen von homopolymerisaten oder copolymerisaten des propylens | |
DE69911555T2 (de) | Verfahren zur herstellung von polymeren | |
DE102004054628A1 (de) | Vorrichtung zur Gasphasenpolymerisation von Olefinen, insbesondere Ethylen | |
DE1442613A1 (de) | Verfahren und Vorrichtung zur Fluidisierung von z.B. Kohle | |
EP0815265B1 (de) | Verfahren zur reduktion von feinerz sowie anlage zur durchführung des verfahrens | |
EP0068146B1 (de) | Verfahren zum Desodorieren feinteiliger, mittels Ziegler-Natta-Katalysatoren erhaltener Propylenpolymerisate | |
DE2524203A1 (de) | Verfahren zur herstellung von hochdruckpolyaethylen | |
DE19904811A1 (de) | Gasphasenwirbelschichtreaktor | |
DE60024743T2 (de) | Verfahren zur Behandlung von teilchenförmigem Material unter Hochdruck | |
DE19821955A1 (de) | Gasphasenwirbelschichtreaktor | |
DE60132884T2 (de) | Olefinpolymerisationsverfahren |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 20001114 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): BE DE ES FI FR GB IT NL SE |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: BASELL POLYOLEFINE GMBH |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: BASELL POLYOLEFINE GMBH |
|
17Q | First examination report despatched |
Effective date: 20040402 |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: KOELLE, PETER Inventor name: ROSENDORFER, PHILIPP Inventor name: FEINDT, HANS-JACOB Inventor name: MICKLITZ, WOLFGANG Inventor name: EVERTZ, KASPAR Inventor name: KARER, RAINER |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: BASELL POLYOLEFINE GMBH |
|
17Q | First examination report despatched |
Effective date: 20040402 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20131203 |