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EP0416242B1 - Installation pour la production d'un gaz à partir de solides carbonifères finement divisés - Google Patents

Installation pour la production d'un gaz à partir de solides carbonifères finement divisés Download PDF

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Publication number
EP0416242B1
EP0416242B1 EP90113136A EP90113136A EP0416242B1 EP 0416242 B1 EP0416242 B1 EP 0416242B1 EP 90113136 A EP90113136 A EP 90113136A EP 90113136 A EP90113136 A EP 90113136A EP 0416242 B1 EP0416242 B1 EP 0416242B1
Authority
EP
European Patent Office
Prior art keywords
product gas
cooling
section
gasification
plant according
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.)
Expired - Lifetime
Application number
EP90113136A
Other languages
German (de)
English (en)
Other versions
EP0416242A1 (fr
Inventor
Michael Lang
Gerhard Wilmer
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.)
Krupp Koppers GmbH
Original Assignee
Krupp Koppers 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
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Publication of EP0416242A1 publication Critical patent/EP0416242A1/fr
Application granted granted Critical
Publication of EP0416242B1 publication Critical patent/EP0416242B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the invention relates to a plant for the production of a product gas from a finely divided carbon carrier, in particular from fine-grained to dusty coal, by pressure gasification, with a vertical reactor with gasification part and radiant cooling boiler, which flows through the reactor from bottom to top, a vertical convection cooling apparatus which is flowed from top to bottom, and a cooled connecting line between the head of the reactor and the head of the convection cooling apparatus, the reactor having a shaft formed from pipes, a lower liquid slag outlet and an upper, drawn-in connecting section for the connecting line and for cooling the product gas to is set up for sufficient solidification of liquid entrained slag particles, the convection cooling apparatus being equipped with a lower outlet for the product gas and for entrained slag particles, and wherein f moreover, the gasification part of the reactor has a lower primary reaction zone and an upper secondary reaction zone.
  • the reaction mainly leads to CO2 and H2 O.
  • a water gas reaction takes place, which leads to the product gas consisting essentially of CO2 and H2.
  • the product gas is obtained as raw product gas and is then cleaned. It is used, for example, as a synthesis gas for the production of hydrocarbons, as a heating gas, in particular for gas turbines, or as a reducing gas for metallurgical purposes.
  • the product gas stream leaves the gasification section at a temperature in the range from 1300 ° C. to 1700 ° C.
  • the aim in this area is a temperature of the product gas at approximately 1400 ° C.
  • the overall height ratios are so balanced in relation to the so-called slag split that the product gas does not entail fine-particle slag and the slag mainly runs off liquid from the gasification part.
  • the overall height of the gasification part is set up in such a way that a sufficiently high gasification efficiency is achieved and the product gas does not entrain fine-particle carbon carriers that are not gassed. If the height of the gasification part were to be reduced in the known systems, the slag split and the gasification efficiency would be adversely affected. The product gas would entrain too much slag and, to a disruptive degree, non-gassed fine carbon carriers.
  • the invention has for its object to provide a system of the intended use described above and the basic structure specified at the outset, the gasification part of which is characterized by a considerable reduction in the overall height, without disturbing impairment of the gasification efficiency and the slag split, without enlarging the cross section of the gasification part .
  • the invention teaches that the gasification part, at least in the region of the secondary reaction zone, has radial bulkheads which are cooled with water and leave a central region free, and that the surface of the bulkheads is provided with pins and is coated with a refractory material.
  • the invention achieves a reduction in the overall height of the gasification part without increasing the cross-section, in that, in deviation from the prevailing building theory, the bulkheads set up as indicated are at least guided into the gasification part.
  • the thermodynamic relationships, in particular the reaction sequence are not significantly disturbed by the cooled bulkheads arranged in the gasification part, although in the gasification part with its significantly reduced overall height, the product gas formed is cooled down to a temperature in the range from 1300 ° C. to 1700 ° C. , preferably to a temperature of about 1400 ° C. This is due on the one hand to the fact that the bulkheads leave a central flow area free.
  • the bulkheads in the gasification part are coated with refractory material in the manner described.
  • the liquid slag that runs off the bulkheads is deposited on these bulkheads.
  • the radiation interaction with the components to be formed depends on the surface temperature of the slag that runs off, which is considerably higher than the temperature of the bulkhead walls or even the cooling pipes in the bulkheads. Otherwise, the radial bulkheads define chambers between them.
  • the spacing of the bulkheads can be chosen such that the cooling influence of the bulkheads on the desired reactions is relatively small even in the center of these chambers between the radial bulkheads, so that the radiation efficiency is not adversely affected.
  • the bulkheads with their leading edges and their coated surfaces increase the slag discharge so that, despite the reduced overall height of the gasification part, the slag split is not impaired, even if the flow rate is relatively high.
  • the secondary reaction zone is drawn into a lower section of the radiation cooling boiler and this section of the radiation cooling boiler also has cooled radial bulkheads which leave a central area free and provided with pins and with a refractory Material are coated.
  • the radial bulkheads from the gasification part are also used lead up to the upper part of the radiation cooling boiler and only in the area of the secondary reaction zone in the gasification part or in the lower part of the radiation cooling boiler with a coating of a refractory material.
  • the overall height of the gasification part can be reduced by half and by more than half. Based on the radiation cooling part, the design can be made such that the gasification part has a height that is approximately a factor of 0.5 to 0.4 less than the height of the radiation cooling part. If you compare the height of the secondary reaction zone in the plant according to the invention with a secondary reaction zone which is of classic design without bulkheads, the height of the embodiment according to the invention is 0.2 to 0.8 times smaller. Operation with significantly improved efficiency and reduced energy losses is possible if the following further measures are implemented in combination with the measures described.
  • the reactor has a shaft, which is designed with respect to the disturbance of the product gas as a constant-speed flow channel into which the cooled bulkheads protrude radially and that of devices for the supply of third parties Coolant is free, and that the constant-velocity flow channel is designed as a radiation cooler with respect to the cooling of the product gas so that the entrained slag is sufficiently solidified solely by the radiation cooling.
  • a foreign coolant is not introduced means that a quench device is not provided in the radiation cooling boiler.
  • the constant-velocity flow channel has a cross section which decreases in the flow direction in accordance with the cooling-related volume reduction of the product gas.
  • the constant-speed flow channel begins in the gasification section immediately above the combustion chambers of the gasification burners.
  • the constant-speed flow channel can also be designed as a flow channel with a cylindrical cross section and as a radiation cooler for cooling the product gas down to about 1300 ° C to 1000 ° C upon entry into the connecting line, a drawn connecting part for the connecting line and / or a quenching device for the introduction of external coolants is then arranged and a subsequent section of the connecting line is set up as a direct cooling section and is designed for cooling the product gas to about 1000 ° C. to 700 ° C.
  • the flow rate of the product gas can be within wide limits in the equipotential flow channel, e.g. B. vary from 0.2 to 20 m / sec.
  • the constant speed flow channel is preferably for a flow speed of the product gas of less than 1 m / sec. set up.
  • the system shown in the figures is used to generate a product gas from a finely divided carbon carrier.
  • a finely divided carbon carrier In particular from fine-grained to dust-like coal or a similar fuel, by means of pressure gasification.
  • Belong to the basic structure a vertical reactor with gasification part 1 and radiation cooling boiler 2, which is flowed through from bottom to top, a vertical convection cooling apparatus 3, which is flowed through from top to bottom and a cooled connecting line 4 between the head of the reactor 1, 2 and the head of the convection cooling apparatus 3.
  • the arrangement is such that the reactor 1, 2 is a substantially circular circular section formed from tubes 5 Has shaft 6, a lower liquid slag outlet 7 and an upper retracted connector 3 for the connecting line 4.
  • the burners 9 are arranged in the lower region of the gasification part 1.
  • the reactor 1, 2 is set up to cool the product gas until sufficient solidified entrained slag particles.
  • the convection cooling apparatus 3 is equipped with a lower vent 10 for the product gas and for entrained slag particles.
  • the gasification part 1 of the reactor has a lower primary reaction zone 11 and an upper secondary reaction zone 12.
  • the secondary reaction zone 12 is drawn into a lower section of the radiation cooling boiler 2 and that this section of the radiation cooling boiler also has guided radial bulkheads 13 which leave a central area 14 free and which are provided with pins 15 provided and coated with a refractory material 16.
  • the radial bulkheads 13 are also in the embodiment from the gasification part 1 to the upper part of the radiation cooling boiler 2, but only in the area of the secondary reaction zone 12 in the gasification part 1 or in the hatched area 17 of the radiation cooling boiler 2 with the pins 15 and a coating made of a refractory material 16.
  • the reactor has a shaft 20 which is designed as a constant-speed flow channel with respect to the flow of the product gas. He is free from facilities for the direct supply of external coolants.
  • the constant-speed flow channel 20 is designed as a radiation cooler with respect to the cooling of the product gas and is designed such that the entrained slag particles are sufficiently solidified solely by the radiation cooling.
  • the constant-speed flow channel 20 is designed as a flow channel which is cylindrical in cross section and is designed as a radiation cooler for cooling the product gas down to approximately 1300 ° C. to 1000 ° C. upon entry into the connecting line 4.
  • a quench device 21 for the direct introduction of external coolants can be seen in the area of the connecting section 8 drawn in in the form of a nozzle for the connecting line 4 and / or in connection thereafter.
  • the connecting line 4 set up as a direct cooling section and designed for cooling the product gas to about 1000 ° C to 7000 ° C.
  • the constant-speed flow channel 20 has a cross section that decreases in the flow direction in accordance with the cooling-related volume reduction of the product gas.
  • the constant-speed flow channel 20 begins immediately above the burners 9, which can otherwise be seen in particular in FIG. 2, which represents a section in the direction AB through the object of FIG. 1. Otherwise, a steam superheater 22 is provided in the exemplary embodiment; it is located in the upper part of the convection cooling apparatus 3. Knock-out cleaning devices 23 are indicated in FIG. 1, which act on the outside of the shaft that forms the constant-speed flow channel 20. However, they can also be recognized by the convection cooling apparatus 3.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Claims (10)

  1. Installation pour fabriquer un gaz produit à partir d'une substance carbonifère finement divisée, en particulier à partir de charbon à grains finement divisé à pulvérulent, par la voie de la gazéification sous pression comprenant :
       un réacteur vertical avec une partie de gazéification et une chaudière de refroidissement par rayonnement, lequel réacteur est parcouru de bas en haut;
       un appareil de refroidissement par convection vertical qui est parcouru de haut en bas; et
       un conduit de raccordement refroidi entre la tête du réacteur et la tête de l'appareil de refroidissement par convection;
       dans laquelle le réacteur comprend une cuve formée de tubes, une sortie de cendres liquides inférieure et une pièce de raccordement supérieure insérée pour le conduit de raccordement et est aussi agencé en vue du refroidissement du gaz produit jusqu'à une solidification suffisante des particules de cendre liquide entraînées, dans laquelle l'appareil de refroidissement par convection est muni d'une sortie inférieure pour le gaz produit et les particules de cendre entraînées et dans laquelle de plus la partie de gazéification du réacteur comprend une zone de réaction primaire inférieure et une zone de réaction secondaire supérieure, caractérisée en ce que la partie de gazéification (1) présente, au moins dans la région de la zone de réaction secondaire (12), des cloisons radiales (13), qui sont refroidies par de l'eau et laissent libre une région centrale (14) et en ce que la surface des cloisons (13) est munie de pointes (15) et revêtue d'une matière réfractaire (16).
  2. Installation suivant la revendication 1, caractérisée en ce que les cloisons (13) s'étendent jusque dans la région de la zone de réaction primaire (11).
  3. Installation suivant l'une quelconque des revendications 1 et 2, caractérisée en ce que la zone de réaction secondaire (12) est prolongée dans une pièce partielle inférieure de la chaudière de refroidissement par rayonnement (2) (région 17) et en ce que cette pièce partielle de la chaudière de refroidissement par rayonnement (2) comprend aussi des cloisons (13) refroidies par de l'eau, qui laissent libre une région centrale (14) et sont munies de pointes (15) et revêtues d'une matière réfractaire (16).
  4. Installation suivant l'une quelconque des revendications 1 à 3, caractérisée en ce que les cloisons radiales (13) s'étendent de la partie de gazéification (1) jusque dans la partie supérieure de la chaudière de refroidissement par rayonnement (2) et sont munies d'un revêtement d'une matière réfractaire (16) uniquement dans la région de la zone de réaction secondaire (12) dans la partie de gazéification ou dans la partie inférieure (région 17) de la chaudière de refroidissement par rayonnement (2).
  5. Installation suivant l'une quelconque des revendications 1 à 4, caractérisée en ce que le gaz produit est conduit dans un séparateur de poussières (19) et les particules de cendre finement divisées d'une teneur élevée en carbone qui y sont déposées sont recyclables à la partie de gazéification (1).
  6. Installation suivant l'une quelconque des revendications 1 à 5, caractérisée en ce que la partie de gazéification (1) a une hauteur construite qui est inférieure d'un facteur d'environ 0,5 à 0,4 à la hauteur construite de la chaudière de refroidissement par rayonnement (2).
  7. Installation suivant l'une quelconque des revendications 1 à 6, caractérisée en ce que le réacteur comprend une cuve (20) qui, sous le rapport de l'écoulement du gaz produit, est réalisée en forme de canal d'écoulement à vitesse constante divisé par les cloisons radiales (13) qui est exempt de dispositifs pour l'apport d'agents de refroidissement étrangers et en ce que le canal d'écoulement à vitesse constante (20) est conçu, sous le rapport du refroidissement du gaz produit, comme réfrigérant par rayonnement de façon qu'une solidification suffisante de la cendre entraînée ait lieu uniquement par le refroidissement par rayonnement.
  8. Installation suivant la revendication 7, caractérisée en ce que le canal d'écoulement à vitesse constante (20) présente une section transversale allant en diminuant dans le sens d'écoulement à mesure de la réduction de volume du gaz produit due au refroidissement et est conçu comme réfrigérant par rayonnement pour un refroidissement du gaz produit d'environ 1000°C jusqu'à 700°C.
  9. Installation suivant l'une quelconque des revendications 7 et 8, caractérisée en ce que le canal d'écoulement à vitesse constante (20) commence immédiatement au-dessus du brûleur (9) de la partie de gazéification (1).
  10. Installation suivant l'une quelconque des revendications 7 à 9, caractérisée en que le canal d'écoulement à vitesse constante (20) est en forme de canal d'écoulement à section cylindrique et est aussi conçu comme réfrigérant par rayonnement pour un refroidissement du gaz produit d'environ 1300°C jusqu'à 1000°C à l'entrée dans le conduit de raccordement (4) et que, dans la région de la pièce de raccordement (8) prolongée et en forme de tube, le conduit de raccordement (4) et/ou un dispositif de refroidissement rapide (21) s'y adaptant sont agencés et une pièce partielle suivante du conduit de raccordement (4) est agencée en trajet de refroidissement direct et conçue pour un refroidissement du gaz produit d'environ 1000°C jusqu'à 700°C.
EP90113136A 1989-09-07 1990-07-10 Installation pour la production d'un gaz à partir de solides carbonifères finement divisés Expired - Lifetime EP0416242B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3929766 1989-09-07
DE3929766A DE3929766A1 (de) 1989-09-07 1989-09-07 Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger

Publications (2)

Publication Number Publication Date
EP0416242A1 EP0416242A1 (fr) 1991-03-13
EP0416242B1 true EP0416242B1 (fr) 1992-12-02

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP90113136A Expired - Lifetime EP0416242B1 (fr) 1989-09-07 1990-07-10 Installation pour la production d'un gaz à partir de solides carbonifères finement divisés

Country Status (10)

Country Link
EP (1) EP0416242B1 (fr)
CN (1) CN1024678C (fr)
CS (1) CS275487B2 (fr)
DD (1) DD297661A5 (fr)
DE (2) DE3929766A1 (fr)
DK (1) DK0416242T3 (fr)
ES (1) ES2036871T3 (fr)
PL (1) PL164182B1 (fr)
TR (1) TR26096A (fr)
ZA (1) ZA905420B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8960651B2 (en) 2008-12-04 2015-02-24 Shell Oil Company Vessel for cooling syngas
US9051522B2 (en) 2006-12-01 2015-06-09 Shell Oil Company Gasification reactor

Families Citing this family (14)

* Cited by examiner, † Cited by third party
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DE4123377A1 (de) * 1991-07-15 1993-01-21 Neumann Siegmar Vorrichtung und verfahren zur reinigung von abgasen bei verbrennungsanlagen mit sortierung der schadstoffe
DE4307462C2 (de) * 1993-03-10 2002-10-17 Krupp Koppers Gmbh Einrichtung für die Vergasung feinkörniger bis staubförmiger Brennstoffe und Verfahren zu deren Betrieb
CN1104625C (zh) * 1995-01-20 2003-04-02 国际壳牌研究有限公司 一种用于冷却载有固体颗粒的热气的装置
DE19649532A1 (de) * 1996-11-29 1998-06-04 Gutehoffnungshuette Man Synthesegas-Wärmetauscher-Anlage
CN101166813B (zh) 2005-05-02 2011-11-23 国际壳牌研究有限公司 生产合成气的方法和系统
DE102005041931B4 (de) * 2005-09-03 2018-07-05 Siemens Aktiengesellschaft Vorrichtung zur Erzeugung von Synthesegasen durch Partialoxidation von aschehaltigen Brennstoffen unter erhöhtem Druck mit Teilquenchung des Rohgases und Abhitzegewinnung
CN101328434B (zh) * 2008-07-17 2011-06-22 中国科学技术大学 一种干煤粉气流床气化炉
EP2334765A2 (fr) 2008-10-08 2011-06-22 Shell Internationale Research Maatschappij B.V. Procédé de préparation d un mélange gazeux d hydrogène et de monoxyde de carbone
AU2009331847B2 (en) 2008-12-22 2012-06-07 Air Products And Chemicals, Inc. Process to prepare methanol and/or dimethylether
US9028571B2 (en) 2011-04-06 2015-05-12 Ineos Bio Sa Syngas cooler system and method of operation
JP5818704B2 (ja) 2012-01-25 2015-11-18 三菱日立パワーシステムズ株式会社 ガス化炉、ガス化発電プラント
CN102851081B (zh) * 2012-09-28 2014-12-31 中国船舶重工集团公司第七一一研究所 一种用水分级激冷的水煤浆或干煤粉气化装置
CN105670708A (zh) * 2016-03-22 2016-06-15 胡志阳 一种合成气冷却的设备和方法
CN109340782B (zh) * 2018-11-27 2024-04-16 湖北金炉节能股份有限公司 一种固体污泥废料焚烧炉

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4610697A (en) * 1984-12-19 1986-09-09 Combustion Engineering, Inc. Coal gasification system with product gas recycle to pressure containment chamber
DE3725424C1 (de) * 1987-07-31 1988-07-21 Steinmueller Gmbh L & C Strahlungskuehler fuer die Abkuehlung von mit Staub beladenen Gasen
DE3844613A1 (de) * 1988-07-16 1990-01-18 Krupp Koppers Gmbh Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger
DE3824233A1 (de) * 1988-07-16 1990-01-18 Krupp Koppers Gmbh Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9051522B2 (en) 2006-12-01 2015-06-09 Shell Oil Company Gasification reactor
US8960651B2 (en) 2008-12-04 2015-02-24 Shell Oil Company Vessel for cooling syngas

Also Published As

Publication number Publication date
PL164182B1 (pl) 1994-06-30
TR26096A (tr) 1994-12-15
ZA905420B (en) 1991-04-24
ES2036871T3 (es) 1993-06-01
CN1024678C (zh) 1994-05-25
DE3929766A1 (de) 1991-03-14
EP0416242A1 (fr) 1991-03-13
PL286686A1 (en) 1991-08-26
CS9004315A3 (en) 1992-02-19
DK0416242T3 (da) 1993-02-22
CN1050039A (zh) 1991-03-20
CS275487B2 (en) 1992-02-19
DE59000540D1 (de) 1993-01-14
DD297661A5 (de) 1992-01-16

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