EP0148799A2 - Process for the gasification of coal and slams - Google Patents

Process for the gasification of coal and slams Download PDF

Info

Publication number
EP0148799A2
EP0148799A2 EP85400018A EP85400018A EP0148799A2 EP 0148799 A2 EP0148799 A2 EP 0148799A2 EP 85400018 A EP85400018 A EP 85400018A EP 85400018 A EP85400018 A EP 85400018A EP 0148799 A2 EP0148799 A2 EP 0148799A2
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
schlamms
fines
coal
gasification
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.)
Granted
Application number
EP85400018A
Other languages
German (de)
French (fr)
Other versions
EP0148799A3 (en
EP0148799B1 (en
Inventor
Serge Delessard
Pierre Henri Sagnier
Pierre Etienne André Palat
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.)
Charbonnages de France CDF
Original Assignee
Charbonnages de France CDF
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 Charbonnages de France CDF filed Critical Charbonnages de France CDF
Publication of EP0148799A2 publication Critical patent/EP0148799A2/en
Publication of EP0148799A3 publication Critical patent/EP0148799A3/en
Application granted granted Critical
Publication of EP0148799B1 publication Critical patent/EP0148799B1/en
Expired legal-status Critical Current

Links

Images

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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam

Definitions

  • the present invention relates to a process for the gasification of coal schlamms in gasification plants in an ash agglomeration fluidized bed.
  • These installations include a reactor in which the coal is maintained in a fluidized bed at a temperature of approximately 900 to 1100 ° C. by injection of water vapor and oxygen at the base of the reactor. Under these conditions, the coal gasifies, while the ash particles formed undergo a start of softening and stick to each other, forming agglomerates. The ashes are separated by a selective withdrawal made possible by the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon, on the other hand, which are not agglomerated. In the installations which are the subject of the cited patents, the separation takes place in one or more venturis located at the base of the reactor.
  • the fluidizing gas is steam and for oxygen to be injected at high speed, mixed with steam, by a tube. located in the center of the venturi, while a gas mainly consisting of water vapor is introduced by the venturi.
  • the jet thus formed in the bed constitutes a hot zone which plays a decisive role in the process of agglomeration of the ash particles.
  • the gases entrain a large quantity of fines constituted, on the one hand, by particles of non-carbonated carbon or incompletely gasified, on the other hand, by ash.
  • These fines are separated, preferably in cyclones, and recycled to the base of the gasification reactor.
  • the flow of fines which is thus continuously recycled is high, for example of the order of 5 times the flow of coal to be gasified.
  • the carbonating carbon is preferably introduced into the upper zone of the fluidized bed, by pneumatic transport, after having been ground to a particle size less than or equal to 6 mm and optionally dried so that its moisture content does not exceed 6%. It may even suffer, as described in US Patent No. 4,057,402, pretreatment at about 400 ° C, so as to reduce its agglutinating properties.
  • German patent N ° 497,894 Even if the process which is the subject of this patent takes advantage of the high temperature of the gases leaving the reactor to achieve partial drying up to about 10% of water and preheating of the product to be gasified, none remains not least that the risks of agglutination and clogging are prohibitive, since the product to be gasified is introduced entirely into the flow leaving the reactor. It is symptomatic to note that, although this patent is very old, the mode of injection which it describes has never been used effectively in the industrial processes which appeared later including in the process developed by the inventors mentioned in this German patent.
  • the schlamms are a by-product of coal preparation plants which are obtained in large quantities in coal wash houses and which cannot be satisfactorily recovered.
  • An object of the present invention is to allow the development of schlamms by gasifying them simultaneously with coal used as main raw material.
  • Another object of the invention is to carry out the gasification of schlamms in an installation such as that which is the subject of European patent application N'0.027.280.
  • a third object of the invention is to take advantage of the latent heat of the products obtained in a gasification reaction in a fluidized bed to dry slurries so as to introduce them in the practically dry state into the lower zone of a fluidized bed.
  • coal gasification By practically dry schlamms is meant a product whose water content is less than 6% by weight and preferably less than 2 to 3% by weight.
  • An additional object of the invention is to dilute the schlamms in the products which are recycled to the gasification reactor, so as to avoid the risks of agglutination and clogging in the injection conduits and to allow this injection without the correct operation of the gasification reactor is disturbed.
  • the invention therefore consists of an improvement to a gasification process in which carbonated carbon is introduced directly into a fluidized bed; oxygen and water vapor are blown into the lower part of the fluidized bed; the ashes are collected in the molten state at the base of the fluidized bed; the products leaving the fluidized bed are successively directed to one or more separation devices for fines and gases and the fines are recycled in the fluidized bed.
  • This improvement consists in injecting schlamms into the circuit of the products which leave the fluidized bed and in introducing the mixture of the dried schlamms and fines separated from the gases in the fluidized bed, preferably directly in the lower part thereof.
  • the schlamms are introduced directly into the gasification reactor, inside the gas phase which overcomes the fluidized bed (disengagement zone).
  • the schlamms are introduced into the flow of hot gases leaving the reactor and before the introduction of this flow into the separation and recycling cycle of the fines.
  • the schlamms are introduced into the circuit or circuits for recycling the fines between the outlet of the separation station (s) for these fines and the reactor.
  • the general reference 1 designates the gasification reactor produced in a manner known per se which it is not necessary to describe here operating in a fluidized bed at a temperature of approximately 900 to 1100 °. C, coal being admitted in 2 and steam and air or oxygen maintaining the fluidization being, respectively, introduced in 3 and 4 at the base of the reactor.
  • the ash particles of the coal thus treated undergo an initial softening and stick together to form agglomerates.
  • Selective removal of the ash is based on the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon which are not agglomerated, on the other hand.
  • the separation takes place in 5 at the base of the reactor and the products are drawn off in 6.
  • the gases resulting from this treatment and which are charged with a large proportion of water vapor and fines with a particle size less than 1 mm are evacuated at 7, at the head of the reactor at a temperature of the order of 1000 ° C. to be admitted, with a view to the separation of these fines, into one or more cyclones such as 8-9.
  • These fines are generally recycled in the reactor 1, respectively, through the conduits 8a-9a. The fraction which would not be recycled could be withdrawn in 10.
  • the schlamms which represent a particle size fraction between 0 and 1 mm are introduced into this gaseous effluent circuit.
  • the schlamms which represent a particle size fraction between 0 and 1 mm are introduced into this gaseous effluent circuit.
  • the schlamms are admitted at 11 into the duct 7 connecting the upper part of the reactor 1 to the first cyclone 8.
  • the schlamms are brought to the temperature of the gas flow and of the fines which circulate there (of the order of 1000 ° C.) to be separated, like these fines, in the cyclone 8 and to be recycled also like the latter, at the same temperature (of the order of 850-900 ° C.) and at the degree of humidity normally prevailing in the recycling duct 8a.
  • the schlamms thus identifying with the fines both in terms of their particle size and the temperature and humidity conditions, it will be understood that they behave like the fines as well when they are admitted to the bottom of the reactor 1 that during their stay in this reactor leading to their gasification without modifying the operating conditions of the installation compared to the case where the schlamms have not been introduced into the fine circuit.
  • full advantage is taken of the sensible heat of the gases leaving the reactor.
  • these schlamms can be introduced into the recycling conduit of one of the cyclones (8-9) in which the conditions of temperature, flow rate and degree of humidity would be the most favorable.
  • we will preferably choose the pipe 8a connected to the first cyclone 8 in which the temperature is the highest (850-900 ° C).
  • we can also admit schlamms in the conduits 9a for the return of fines from cyclone 9 in which the temperature is still around 750-800 ° C (lower than that of conduit 8a) and the flow rate obviously lower to that in conduit 8a.
  • the point of admission thus depends as seen from the number of cyclones and the temperature and flow conditions.
  • the sensible heat leaving the reactor since the sensible heat leaving the reactor is not taken full advantage of, it may be advantageous to at least partially dry the slabs before their introduction into the conduit. In any event, it is advantageous to take advantage of points in the installation where these parameters have optimal values, in particular the temperature.
  • the proportion of schlamms admitted will be eminently a function of the proportion of fines recycled (proportion which is important as indicated above). This proportion may be, depending on the case, of the order of 20 / and up to 50% by weight of the quantity of carbonated carbon.

Landscapes

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

Abstract

1. A process of coal gasification in which coal, as a principal primary material, is introduced directly into a fluidized bed into the lower part of which oxygen and water vapour are blown, ash being recovered in the molten state at the bottom of the bed, whilst the products, on emerging, are successively directed to one or more devices for separating fines and gases, the fines being recycled to the fluidized bed, an improvement in the process with regard to the gasification and to increasing the usefulness of sludges being characterized in that it consists in introducing into the circuit of the products which leave the said fluidized bed at least 20 %, and at most 50 %, by weight of the amount of coal introduced into the installation, of sludges representing a fraction having a grain size comprised between 0 and 1 mm, and of introducing into the fluidized bed a mixture of these dried sludges and of the fines of the same grain size separated from the gases.

Description

La présente invention concerne un procédé pour la gazéification de schlamms de charbon dans les installations de gazéification en lit fluidisé à agglomération de cendres.The present invention relates to a process for the gasification of coal schlamms in gasification plants in an ash agglomeration fluidized bed.

Des installations de ce genre sont, par exemple, celles qui sont décrites dans les brevet US N°2.906.608, N° 3.867.110, N° 3.884.649. N° 3.935.825, N° 4.023.280, N° 4.057. 402, N° 4.191.539, N° 4.229.289. et les demandes de brevets européens N° 0.027.280 et 0.031.856.Installations of this kind are, for example, those described in US Pat. Nos. 2,906,608, No. 3,867,110, No. 3,884,649. N ° 3.935.825, N ° 4.023.280, N ° 4.057. 402, N ° 4.191.539, N ° 4.229.289. and European patent applications Nos. 0.027.280 and 0.031.856.

Ces installations comportent un réacteur dans lequel le charbon est maintenu en lit fluidisé à une température d'environ 900 à 1100°C par injection de vapeur d'eau et d'oxygène à la base du réacteur. Dans ces conditions, le charbon se gazéifie, tandis que les particules de cendres formées subissent un début de ramollissement et se collent entre elles en formant des agglomérats. Les cendres sont séparées par un soutirage sélectif rendu possible par la différence de taille et de densité entre ces agglomérats, d'une part, et les particules contenant encore du carbone, d'autre part, qui ne sont pas agglomérées. Dans les installations faisant l'objet des brevets cités, la séparation s'opère dans un ou plusieurs venturis situés à la base du réacteur.These installations include a reactor in which the coal is maintained in a fluidized bed at a temperature of approximately 900 to 1100 ° C. by injection of water vapor and oxygen at the base of the reactor. Under these conditions, the coal gasifies, while the ash particles formed undergo a start of softening and stick to each other, forming agglomerates. The ashes are separated by a selective withdrawal made possible by the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon, on the other hand, which are not agglomerated. In the installations which are the subject of the cited patents, the separation takes place in one or more venturis located at the base of the reactor.

Selon la demande de brevet européen N°0.027.280, il est avantageux que le gaz de fluidisation soit de la vapeur d'eau et que l'oxygène soit injecté à grande vitesse, mélangé à de la vapeur d'eau, par un tube situé au centre du venturi, tandis qu'un gaz constitué principalement de vapeur d'eau est introduit par le venturi. Le jet ainsi formé dans le lit constitue une zone chaude qui joue un rôle déterminant dans le processus d'agglomération des particules de cendres.According to European patent application No. 0.027.280, it is advantageous for the fluidizing gas to be steam and for oxygen to be injected at high speed, mixed with steam, by a tube. located in the center of the venturi, while a gas mainly consisting of water vapor is introduced by the venturi. The jet thus formed in the bed constitutes a hot zone which plays a decisive role in the process of agglomeration of the ash particles.

A la partie supérieure du lit fluidisé, les gaz entrainent une quantité importante de fines constituées, d'une part, par des particules de charbon non gazéifiées ou incomplètement gazéifiées, d'autre part, par des cendres. Ces fines sont séparées, de préférence dans des cyclones, et recyclées à la base du réacteur de gazéification. Le débit de fines qui est ainsi continuellement recyclé est élevé, par exemple de l'ordre de 5 fois le débit du charbon à gazéifier.At the upper part of the fluidized bed, the gases entrain a large quantity of fines constituted, on the one hand, by particles of non-carbonated carbon or incompletely gasified, on the other hand, by ash. These fines are separated, preferably in cyclones, and recycled to the base of the gasification reactor. The flow of fines which is thus continuously recycled is high, for example of the order of 5 times the flow of coal to be gasified.

Le charbon à gazéifier est de préférence introduit dans la zone supérieure du lit fluidisé, par transport pneumatique, après avoir été broyé à une granulométrie inférieure ou égale à 6 mm et éventuellement séché de manière que sa teneur en humidité ne dépasse pas 6 %. Il peut même subir, comme il est décrit dans le brevet US N° 4.057.402, un prétraitement à environ 400*C, de manière à diminuer ses propriétés agglutinantes.The carbonating carbon is preferably introduced into the upper zone of the fluidized bed, by pneumatic transport, after having been ground to a particle size less than or equal to 6 mm and optionally dried so that its moisture content does not exceed 6%. It may even suffer, as described in US Patent No. 4,057,402, pretreatment at about 400 ° C, so as to reduce its agglutinating properties.

Les installations décrites ci-dessus ne sont pas adaptées à la gazéification de schlamms de lavoirs à charbon. Ces schlamms sont en effet des produits de granulométrie très fine (inférieure à 1 mm) très humide (environ 25 % d'eau après essorage) et dont la teneur en cendres peut atteindre 40 % .The facilities described above are not suitable for the gasification of schlamms of coal wash houses. These schlamms are indeed very fine grain size products (less than 1 mm) very wet (about 25% of water after spinning) and whose ash content can reach 40%.

Les dispositifs classiques d'introduction du charbon dans le réacteur ne sont pas favorables à l'introduction de schlamms, en raison même de cette forte teneur en humidité. Par ailleurs, si on introduit des schlamms dans. la zone supérieure du lit fluidisé, les particules très fines qui les constituent seront entrainées hors du lit avant d'avoir pu être gazéifiées et le fonctionnement du lit sera perturbé sans résultat. La demande de brevet européen N° 0.031.856 a certes prévu une installation permettant d'introduire le charbon à gazéifier à la partie inférieure du lit fluidisé. Toutefois, le procédé décrit dans cette demande de brevet est délicat à mettre en oeuvre, car il faut éviter une agglutination du charbon dans les canalisations d'injection et, par ailleurs, l'introduction massive de produits froids à la base du lit fluidisé n'est pas favorable au bon fonctionnement du réaçteur de gazéification. En outre, un tel dispositif n'est pas adapté à l'injection d'un produit très humide tel que les schlamms de charbon.Conventional devices for introducing coal into the reactor are not favorable to the introduction of schlamms, because of this high moisture content. On the other hand, if we introduce schlamms in. the upper zone of the fluidized bed, the very fine particles which constitute them will be entrained out of the bed before being able to be gasified and the operation of the bed will be disturbed without result. European patent application No. 0.031.856 has certainly provided an installation for introducing carbonated carbonation at the bottom of the fluidized bed. However, the process described in this patent application is difficult to implement, because it is necessary to avoid agglutination of coal in the injection pipes and, moreover, the massive introduction of cold products at the base of the fluidized bed is not favorable for the proper functioning of the gasification reactor. In addition, such a device is not suitable for injecting a very wet product such as carbon schlamms.

Les mêmes inconvénients se retrouvent dans le brevet allemand N° 497.894. Même si le procédé faisant l'objet de ce brevet met à profit la température élevée des gaz qui sortent du réacteur pour réaliser un séchage partiel jusqu'à environ 10 % d'eau et un préchauffage du produit à gazéifier, il n'en demeure pas moins que les risques d'agglutination et de colmatage sont prohibitifs, étant donné que le produit à gazéifier est introduit en totalité dans le flux sortant du réacteur. Il est symptomatique de constater que, bien que ce brevet soit très ancien, le mode d'injection qu'il décrit n'a jamais été utilisé effectivement dans les procédés industriels qui sont apparus ultérieurement y compris dans le procédé développé par les inventeurs mentionnés dans ce brevet allemand.The same drawbacks are found in German patent N ° 497,894. Even if the process which is the subject of this patent takes advantage of the high temperature of the gases leaving the reactor to achieve partial drying up to about 10% of water and preheating of the product to be gasified, none remains not least that the risks of agglutination and clogging are prohibitive, since the product to be gasified is introduced entirely into the flow leaving the reactor. It is symptomatic to note that, although this patent is very old, the mode of injection which it describes has never been used effectively in the industrial processes which appeared later including in the process developed by the inventors mentioned in this German patent.

Les schlamms constituent un sous-produit des installations de préparation du charbon que l'on obtient en grande quantité dans les lavoirs à charbon et que l'on ne sait pas valoriser de façon satisfaisante.The schlamms are a by-product of coal preparation plants which are obtained in large quantities in coal wash houses and which cannot be satisfactorily recovered.

Un but de la présente invention est de permettre la valorisation des schlamms en les gazéifiant simultanément avec du charbon utilisé à titre de matière première principale.An object of the present invention is to allow the development of schlamms by gasifying them simultaneously with coal used as main raw material.

Un autre but de l'invention est de réaliser la gazéification de schlamms dans une installation telle que celle qui fait l'objet de la demande de brevet européen N'0.027.280.Another object of the invention is to carry out the gasification of schlamms in an installation such as that which is the subject of European patent application N'0.027.280.

un troisième but de 1 invention est de mettre à profit la chaleur latente des produits obtenus dans une réaction de gazéification en lit fluidisé pour sécher des schlamms de manière à les introduire à l'état pratiquement sec dans la zone inférieure d'un lit fluidisé. de gazéification de charbon. Par schlamms pratiquement secs, on entend un produit dont la teneur en eau est inférieure à 6 % en poids et de préférence inférieure à 2 à 3 % en poids.a third object of the invention is to take advantage of the latent heat of the products obtained in a gasification reaction in a fluidized bed to dry slurries so as to introduce them in the practically dry state into the lower zone of a fluidized bed. coal gasification. By practically dry schlamms is meant a product whose water content is less than 6% by weight and preferably less than 2 to 3% by weight.

Un but supplémentaire de l'invention est de diluer les schlamms dans les produits qui sont recyclés au réacteur de gazéification, de manière à éviter les risques d'agglutination et de colmatage dans les conduits d'injection et à permettre cette injection sans que le bon fonctionnement du réacteur de gazéification ne soit perturbé.An additional object of the invention is to dilute the schlamms in the products which are recycled to the gasification reactor, so as to avoid the risks of agglutination and clogging in the injection conduits and to allow this injection without the correct operation of the gasification reactor is disturbed.

Ces buts sont atteints dans un procédé de gazéification tel que celui qui fait l'objet de la demande de brevet européen N* 0.027.280. par le fait que l'on injecte des schlamms de charbon en proportion inférieure à 50 X en poids et de préférence de l'ordre de 20 % en poids du débit de charbon introduit dans l'installation (proportion qui correspond à la production usuelle des schlamms obtenus dans un lavoir à charbon à partir du charbon tout venant) dans le circuit des produits qui sortent du lit fluidisé où s'effectue la réaction de gazéification.These aims are achieved in a gasification process such as that which is the subject of European patent application N * 0.027.280. by the fact that coal schlamms are injected in a proportion less than 50% by weight and preferably of the order of 20% by weight of the flow of coal introduced into the installation (proportion which corresponds to the usual production of schlamms obtained in a coal washing plant from coarse coal) in the circuit of the products which leave the fluidized bed where the gasification reaction takes place.

L'invention consiste par conséquent en un perfectionnement à un procédé de gazéification dans lequel du charbon à gazéifier est introduit directement dans un lit fluidisé ; de l'oxygène et de la vapeur d'eau sont insufflés à la partie inférieure du lit fluidisé ; les cendres sont recueillies à l'état fondu à la base du lit fluidisé ; les produits sortant du lit fluidisé sont dirigés successivement vers un ou plusieurs dispositifs de séparation des fines et des gaz et les fines sont recyclées dans le lit fluidisé.The invention therefore consists of an improvement to a gasification process in which carbonated carbon is introduced directly into a fluidized bed; oxygen and water vapor are blown into the lower part of the fluidized bed; the ashes are collected in the molten state at the base of the fluidized bed; the products leaving the fluidized bed are successively directed to one or more separation devices for fines and gases and the fines are recycled in the fluidized bed.

Ce perfectionnement consiste à injecter des schlamms dans le circuit des produits qui sortent du lit fluidisé et à introduire le mélange des schlamms séchés et des fines séparées des gaz dans le lit fluidisé, de préférence directement dans la partie inférieure de celui-ci..This improvement consists in injecting schlamms into the circuit of the products which leave the fluidized bed and in introducing the mixture of the dried schlamms and fines separated from the gases in the fluidized bed, preferably directly in the lower part thereof.

Suivant le mode de réalisation préféré de l'invention, les schlamms sont introduits directement dans le réacteur de gazéification, à l'intérieur de la phase gazeuse qui surmonte le lit fluidisé (zone de désengagement).According to the preferred embodiment of the invention, the schlamms are introduced directly into the gasification reactor, inside the gas phase which overcomes the fluidized bed (disengagement zone).

Suivant un autre mode de réalisation avantageux, les schlamms sont introduits dans le flux de gaz chauds sortant du réacteur et avant l'introduction de ce flux dans le cycle de séparation et de recyclage des fines.According to another advantageous embodiment, the schlamms are introduced into the flow of hot gases leaving the reactor and before the introduction of this flow into the separation and recycling cycle of the fines.

Suivant un autre mode de réalisation possible, les schlamms sont introduits dans le ou les circuits de recyclage des fines entre la sortie du ou des postes de séparation de ces fines et le réacteur.According to another possible embodiment, the schlamms are introduced into the circuit or circuits for recycling the fines between the outlet of the separation station (s) for these fines and the reactor.

D'autres caractéristiques et les avantages de l'invention ressortiront plus clairement de la description qui va suivre faite en regard du dessin annexé représentant à titre illustratif et schématiquement le réacteur d'une installation de type connu de gazéification de charbon en lit fluidisé et à agglomération de cendres, réacteur auquel est appliqué le procédé de l'invention.Other characteristics and advantages of the invention will emerge more clearly from the description which follows, given with regard to the appended drawing representing by way of illustration and schematically the reactor of an installation of known type of gasification of coal in a fluidized bed and at agglomeration of ash, reactor to which the process of the invention is applied.

En se référant à ce schéma, on a désigné par la référence générale 1 le réacteur de gazéification réalisé de façon connue en soi qu'il n'est pas nécessaire de décrire ici fonctionnant en lit fluidisé à une température d'environ 900 à 1100°C, le charbon étant admis en 2 et la vapeur et l'air ou l'oxygène entretenant la fluidisation étant, respectivement, introduits en 3 et 4 à la base du réacteur. Comme on le sait, dans ces conditions, les particules de cendres du charbon ainsi traité subissent un début de ramollissement et se collent entre elles pour former des agglomérats. Le soutirage sélectif des cendres repose sur la différence de taille et de densité entre ces agglomérats, d'une part, et les particules contenant encore du carbone qui ne sont pas agglomérées, d'autre part. La séparation s'opère en 5 à la base du réacteur et les produits sont soutirés en 6. Les gaz résultant de ce traitement et qui sont chargés d'une proportion importante de vapeur d'eau et de fines d'une granulométrie inférieure à 1 mm sont évacués en 7, en tête du réacteur à une température de l'ordre de 1000'C pour être admis, en vue de la séparation de ces fines, dans un ou plusieurs cyclones tels que 8-9. Ces fines sont en général recyclées dans le réacteur 1, respectivement, par les conduits 8a-9a. La fraction qui ne serait pas recyclée pourrait être soutirée en 10.With reference to this diagram, the general reference 1 designates the gasification reactor produced in a manner known per se which it is not necessary to describe here operating in a fluidized bed at a temperature of approximately 900 to 1100 °. C, coal being admitted in 2 and steam and air or oxygen maintaining the fluidization being, respectively, introduced in 3 and 4 at the base of the reactor. As we knows, under these conditions, the ash particles of the coal thus treated undergo an initial softening and stick together to form agglomerates. Selective removal of the ash is based on the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon which are not agglomerated, on the other hand. The separation takes place in 5 at the base of the reactor and the products are drawn off in 6. The gases resulting from this treatment and which are charged with a large proportion of water vapor and fines with a particle size less than 1 mm are evacuated at 7, at the head of the reactor at a temperature of the order of 1000 ° C. to be admitted, with a view to the separation of these fines, into one or more cyclones such as 8-9. These fines are generally recycled in the reactor 1, respectively, through the conduits 8a-9a. The fraction which would not be recycled could be withdrawn in 10.

Conformément à l'invention, les schlamms qui représentent une fraction granulométrique comprise entre 0 et 1 mm sont introduits dans ce circuit d'effluent gazeux. En raison même de cette granulométrie, ils sont compatibles avec le reste des fines de même granulométrie qui sont entrainées par cet effluent ou qui en sont séparées.According to the invention, the schlamms which represent a particle size fraction between 0 and 1 mm are introduced into this gaseous effluent circuit. By reason of this granulometry, they are compatible with the rest of the fines of the same granulometry which are entrained by this effluent or which are separated from it.

C'est ainsi que, suivant un premier mode de mise en oeuvre de l'invention, les schlamms sont admis en 11 dans le conduit 7 reliant la partie supérieure du réacteur 1 au premier cyclone 8.Thus, according to a first embodiment of the invention, the schlamms are admitted at 11 into the duct 7 connecting the upper part of the reactor 1 to the first cyclone 8.

Quels que soient la température ou le débit d'admission de ces schlamms dans ce conduit, il y a tout d'abord lieu de remarquer qu'ils n'interfèrent en rien dans la marche du réacteur. Par ailleurs, comme indiqué précédemment, leur granulométrie permet de les assimiler aux fines normalement évacuées du réacteur 1. En outre, cette admission n'entrave en rien la marche des cyclones 8 et 9 destinés à la séparation de cette fraction de granulométrie.Whatever the temperature or the flow rate of these schlamms in this duct, it should first of all be noted that they do not interfere in any way in the operation of the reactor. Furthermore, as indicated above, their particle size makes it possible to assimilate them to the fines normally discharged from reactor 1. In addition, this admission does not in any way hamper the operation of cyclones 8 and 9 intended for the separation of this particle size fraction.

En ce qui concerne le débit d'admission des schlamms, il peut être élevé du fait même que ces cyclones sont prévus pour permettre la séparation d'une quantité de fines importante de l'ordre de 5 fois (ou plus) la quantité de charbon admise dans le réacteur.Regarding the inlet flow of the schlamms, it can be high because these cyclones are designed to allow the separation of a large quantity of fines of the order of 5 times (or more) the quantity of coal admitted into the reactor.

. Lors de leur cheminement dans le conduit 7, les schlamms sont amenés à la température du flux gazeux et des fines qui y circulent (de l'ordre de 1000°C) pour être séparés, comme ces fines, dans le cyclone 8 et être recyclés également comme ces dernières, à la même température (de l'ordre de 850-900'C) et au degré d'humidité régnant normalement dans le conduit de recyclage 8a. Les schlamms s'identifiant ainsi aux fines aussi bien pour ce qui est de leur granulométrie que des conditions de température et de taux d'humidité, on comprendra qu'ils se comportent comme les fines aussi bien lors de leur admission au bas du réacteur 1 qu'au cours de leur séjour au sein de ce réacteur conduisant à leur gazéification sans modification des conditions de marche de l'installation par rapport au cas où les schlamms n'auraient pas été introduits dans le circuit des fines. Dans cette variante, on profite pleinement de la chaleur sensible des gaz sortant du réacteur.. During their passage in the conduit 7, the schlamms are brought to the temperature of the gas flow and of the fines which circulate there (of the order of 1000 ° C.) to be separated, like these fines, in the cyclone 8 and to be recycled also like the latter, at the same temperature (of the order of 850-900 ° C.) and at the degree of humidity normally prevailing in the recycling duct 8a. The schlamms thus identifying with the fines both in terms of their particle size and the temperature and humidity conditions, it will be understood that they behave like the fines as well when they are admitted to the bottom of the reactor 1 that during their stay in this reactor leading to their gasification without modifying the operating conditions of the installation compared to the case where the schlamms have not been introduced into the fine circuit. In this variant, full advantage is taken of the sensible heat of the gases leaving the reactor.

Suivant une variante, ces schlamms peuvent être introduits dans le conduit de recyclage d'un des cyclones (8-9) dans lequel les conditions de température, de débit et de degré d'humidité seraient les plus favorables. Dans le cas pris comme exemple ici, on choisira de préférence le conduit 8a relié au premier cyclone 8 dans lequel la température est la plus élevée (850-900°C). Bien entendu, on pourra également admettre les schlamms dans les conduits 9a de retour des fines provenant du cyclone 9 dans lequel la température est encore de l'ordre de 750-800°C (inférieure à celle du conduit 8a) et le débit inférieur évidemment à celui dans le conduit 8a. Le point d'admission dépend ainsi comme on le voit du nombre de cyclones et des conditions de température et de débit. Dans cette variante, étant donné qu'on ne profite pas pleinement de la chaleur sensible sortant du réacteur, il peut être avantageux de sécher au moins partiellement les schlamms avant leur introduction dans le conduit. En tout état de cause, il y a intérêt à profiter des points de l'installation où ces paramètres ont des valeurs optimales notamment la température. Pour ce qui est du débit, les schlamms constituant un appoint par rapport au débit de charbon initial à gazéifier, la proportion de schlamms admise sera éminemment fonction de la proportion de fines recyclées (proportion qui est importante comme indiqué ci-dessus). Cette proportion pourra être suivant les cas de l'ordre de 20 / et jusqu'à 50 X en poids de la quantité de charbon gazéifié.According to a variant, these schlamms can be introduced into the recycling conduit of one of the cyclones (8-9) in which the conditions of temperature, flow rate and degree of humidity would be the most favorable. In the case taken as an example here, we will preferably choose the pipe 8a connected to the first cyclone 8 in which the temperature is the highest (850-900 ° C). Of course, we can also admit schlamms in the conduits 9a for the return of fines from cyclone 9 in which the temperature is still around 750-800 ° C (lower than that of conduit 8a) and the flow rate obviously lower to that in conduit 8a. The point of admission thus depends as seen from the number of cyclones and the temperature and flow conditions. In this variant, since the sensible heat leaving the reactor is not taken full advantage of, it may be advantageous to at least partially dry the slabs before their introduction into the conduit. In any event, it is advantageous to take advantage of points in the installation where these parameters have optimal values, in particular the temperature. With regard to the flow rate, the schlamms constituting an addition to the initial coal flow rate to be gasified, the proportion of schlamms admitted will be eminently a function of the proportion of fines recycled (proportion which is important as indicated above). This proportion may be, depending on the case, of the order of 20 / and up to 50% by weight of the quantity of carbonated carbon.

Elle sera nettement plus faible lorsque les schlamms sont introduits dans le circuit de recyclage du second cyclone, ou à plus forte raison du troisième, s'il en existe trois. Elle sera alors déterminée par les conditions d'hydrodynamique du système, de manière à assurer un écoulement régulier dans la jambe de retour. Elle sera également limitée en fonction des risques d'agglutination dans ce circuit liés aux caractéristiques du charbon.It will be much lower when the schlamms are introduced into the recycling circuit for the second cyclone, or even more so for the third, if there are three. It will then be determined by the hydrodynamic conditions of the system, so as to ensure a smooth flow in the return leg. It will also be limited according to the risks of agglutination in this circuit linked to the characteristics of the coal.

Il va de soi que la présente invention n'a été décrite qu'à titre purement explicatif et nullement limitatif et que toute modification utile pourra y être apportée sans sortir de son cadre.It goes without saying that the present invention has been described for purely explanatory and in no way limitative and that any useful modification may be made without departing from its scope.

Claims (5)

1. Perfectionnement au procédé pour la gazéification du charbon en vue de la gazéification de schlamms, dans lequel le charbon à gazéifier est introduit directement dans un lit fluidisé ; de l'oxygène et de la vapeur d'eau sont insufflés à la partie inférieure du lit fluidisé ; les cendres sont recueillies à l'état fondu à la base du lit fluidisé ; les produits sortant du lit fluidisé sont dirigés successivement vers un ou plusieurs dispositifs de séparation des fines et des gaz et les fines sont recyclées dans le lit fluidisé, perfectionnement en vue de la gazéification des schlamms, caractérisé par le fait qu'il consiste à injecter des schlamms dans le circuit des produits qui sortent du lit fluidisé et à introduire le mélange des schlamms séchés et des fines séparées des gaz dans le lit fluidisé.1. Improvement of the process for the gasification of coal with a view to the gasification of schlamms, in which the coal to be gasified is introduced directly into a fluidized bed; oxygen and water vapor are blown into the lower part of the fluidized bed; the ashes are collected in the molten state at the base of the fluidized bed; the products leaving the fluidized bed are directed successively to one or more separation devices for fines and gases and the fines are recycled in the fluidized bed, an improvement with a view to the gasification of schlamms, characterized in that it consists in injecting schlamms in the circuit of the products which leave the fluidized bed and to introduce the mixture of the dried schlamms and fines separated from the gases in the fluidized bed. 2. Perfectionnement selon la revendication 1, caractérisé par le fait que cette injection se fait directement dans la partie inférieure du lit fluidisé.2. Improvement according to claim 1, characterized in that this injection takes place directly in the lower part of the fluidized bed. 3. Perfectionnement selon la revendication 1, caractérisé par le fait que les schlamms sont introduits directement dans le réacteur de gazéification, à l'intérieur de la phase gazeuse qui surmonte le lit fluidisé.3. Improvement according to claim 1, characterized in that the schlamms are introduced directly into the gasification reactor, inside the gas phase which overcomes the fluidized bed. 4. Perfectionnement selon la revendication 1, caractérisé par le fait que les schlamms sont introduits dans le flux de gaz chauds sortant du réacteur et avant l'introduction de ce flux dans le cycle de séparation et de recyclage des fines.4. Improvement according to claim 1, characterized in that the schlamms are introduced into the flow of hot gases leaving the reactor and before the introduction of this flow into the separation and recycling cycle of fines. 5. Perfectionnement selon la revendication 1, caractérisé par le fait que les schlamms sont introduits dans le ou les circuits de recyclage des fines entre la sortie du ou des postes de séparation de ces fines et le réacteur.5. Improvement according to claim 1, characterized in that the schlamms are introduced into the circuit or circuits for recycling the fines between the outlet of the separation station (s) for these fines and the reactor.
EP19850400018 1984-01-10 1985-01-07 Process for the gasification of coal and slams Expired EP0148799B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8400285 1984-01-10
FR8400285A FR2557885B1 (en) 1984-01-10 1984-01-10 PROCESS FOR THE GASIFICATION OF SCHLAMMS

Publications (3)

Publication Number Publication Date
EP0148799A2 true EP0148799A2 (en) 1985-07-17
EP0148799A3 EP0148799A3 (en) 1986-06-11
EP0148799B1 EP0148799B1 (en) 1989-05-24

Family

ID=9299969

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19850400018 Expired EP0148799B1 (en) 1984-01-10 1985-01-07 Process for the gasification of coal and slams

Country Status (5)

Country Link
EP (1) EP0148799B1 (en)
CN (1) CN85101391A (en)
DE (1) DE3570453D1 (en)
FR (1) FR2557885B1 (en)
IN (1) IN163507B (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2593496A1 (en) * 1986-01-30 1987-07-31 Korf Engineering Gmbh PROCESS FOR GASIFYING CURING SLUDGE
EP0708168A1 (en) * 1994-10-17 1996-04-24 N.V. Kema Method and installation for gasifying solid fuel
CN103881782A (en) * 2014-04-09 2014-06-25 河南理工大学 Fluidized-bed gasifier fly ash granules and production method thereof

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8172164B2 (en) * 2009-02-27 2012-05-08 General Electric Company Method and apparatus for a feed into a gasifier utilizing a slurry

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE497894C (en) * 1930-05-15 I G Farbenindustrie Akt Ges Process for producing water gas and other flammable gases
GB401463A (en) * 1932-09-01 1933-11-16 Ig Farbenindustrie Ag Improvements in and apparatus for the gasification of finelygrained moist fuels
DE1074803B (en) * 1960-02-04 Badische Anilin- &. Soda-Fabrik Aktiengesellschaft, Ludwigshafen/Rhein Process for generating fuel gas by gasifying finely divided solid or liquid fuels and / or by splitting gaseous fuels in a fluidized bed
GB1558996A (en) * 1976-07-27 1980-01-09 Gulf Oil Corp Fliud bed gasifier
EP0027280A1 (en) * 1979-10-15 1981-04-22 Institute of Gas Technology Process and apparatus for the conversion of agglomerating hydrocarbonaceous solid material to a more valuable gaseous product
DE3004111A1 (en) * 1980-02-05 1981-08-13 Hölter, Heinz, Ing.(grad.), 4390 Gladbeck Coal-refuse mixt. utilisation - by pyrolysis followed by crushing and fluidised bed combustion
FR2493333A1 (en) * 1980-10-31 1982-05-07 Nippon Kokan Kk COAL GASIFYING APPARATUS USING COAL POWDER

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE497894C (en) * 1930-05-15 I G Farbenindustrie Akt Ges Process for producing water gas and other flammable gases
DE1074803B (en) * 1960-02-04 Badische Anilin- &. Soda-Fabrik Aktiengesellschaft, Ludwigshafen/Rhein Process for generating fuel gas by gasifying finely divided solid or liquid fuels and / or by splitting gaseous fuels in a fluidized bed
GB401463A (en) * 1932-09-01 1933-11-16 Ig Farbenindustrie Ag Improvements in and apparatus for the gasification of finelygrained moist fuels
GB1558996A (en) * 1976-07-27 1980-01-09 Gulf Oil Corp Fliud bed gasifier
EP0027280A1 (en) * 1979-10-15 1981-04-22 Institute of Gas Technology Process and apparatus for the conversion of agglomerating hydrocarbonaceous solid material to a more valuable gaseous product
DE3004111A1 (en) * 1980-02-05 1981-08-13 Hölter, Heinz, Ing.(grad.), 4390 Gladbeck Coal-refuse mixt. utilisation - by pyrolysis followed by crushing and fluidised bed combustion
FR2493333A1 (en) * 1980-10-31 1982-05-07 Nippon Kokan Kk COAL GASIFYING APPARATUS USING COAL POWDER

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2593496A1 (en) * 1986-01-30 1987-07-31 Korf Engineering Gmbh PROCESS FOR GASIFYING CURING SLUDGE
GB2185970A (en) * 1986-01-30 1987-08-05 Korf Engineering Gmbh Process for the gasification of sewage sludge
GB2185970B (en) * 1986-01-30 1990-03-21 Korf Engineering Gmbh Process for the gasification of sewage sludge
EP0708168A1 (en) * 1994-10-17 1996-04-24 N.V. Kema Method and installation for gasifying solid fuel
CN103881782A (en) * 2014-04-09 2014-06-25 河南理工大学 Fluidized-bed gasifier fly ash granules and production method thereof

Also Published As

Publication number Publication date
IN163507B (en) 1988-10-01
DE3570453D1 (en) 1989-06-29
CN85101391A (en) 1987-01-31
EP0148799A3 (en) 1986-06-11
FR2557885B1 (en) 1987-07-17
EP0148799B1 (en) 1989-05-24
FR2557885A1 (en) 1985-07-12

Similar Documents

Publication Publication Date Title
EP0161970B1 (en) Method and installation for the treatment of material in a circulating fluidized bed
US3957459A (en) Coal gasification ash removal system
AU2011336788B2 (en) Method and apparatus for particle recycling in multiphase chemical reactors
EP0173782B1 (en) Process for treating materials
EP2633003B1 (en) Production of synthesis gas by heating oxidized biomass with a hot gas obtained from the oxidation of residual products
FR2851570A1 (en) INSTALLATION AND METHOD FOR MULTI-STAGE GASIFICATION OF A LOAD COMPRISING ORGANIC MATTER
FR2483258A1 (en) PROCESS FOR REMOVING SOLID WASTE
FR2593496A1 (en) PROCESS FOR GASIFYING CURING SLUDGE
US3847566A (en) Fluidized bed gasification process with reduction of fines entrainment by utilizing a separate transfer line burner stage
EP0148799B1 (en) Process for the gasification of coal and slams
EP1137591B1 (en) Partial oxidation process with soot filter cake recovery
WO2017103527A1 (en) Process for the fluidized-bed gasification of tyres
FR2546288A1 (en) METHOD FOR RECOVERING HEAT FROM GASES CONTAINING SUBSTANCES CONTAMINATING HEAT TRANSFER SURFACES
EP4257660A2 (en) Process and apparatus for producing synthesis gas through thermochemical conversion of biomass and waste materials
FR2505808A1 (en) PREPARATION OF SYNTHESIS GAS FROM HYDROCARBONS RICH IN ASH
AU2006211317B2 (en) Apparatus and method for gasifying solid fuel
FR2535017A1 (en) PROCESS FOR THE COMBUSTION OF COKE PRESENT ON SOLID PARTICLES AND FOR THE PRODUCTION OF HEAT RECOVERABLE FROM PARTICLES CONTAINING HYDROCARBONS AND APPARATUS FOR CARRYING OUT SAID METHOD
EP4293093A1 (en) Process and process plant for converting feedstock comprising a carbon-containing solid fuel
FR2683829A1 (en) IRON ORE REDUCTION TREATMENT FACILITY IN FLUIDIZING BED CIRCULATING.
JPS5884890A (en) Rotary kiln coal gas generator for removing dust from gas by injecting tar
FR2529221A1 (en) METHOD AND APPARATUS FOR GASIFICATION USING COAL, COKE OR THE LIKE
FR2556002A1 (en) PROCESS AND PLANT FOR THE REDUCTION OF OXIDIZED MATERIAL, WITH SIMULTANEOUS GENERATION OF A GAS SUITABLE AS FUEL GAS
BE815592A (en) Fluidised-bed heat treatment of bituminous coal - for conversion into particles for active carbon prodn
BE468700A (en)
BE676638A (en)

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

AK Designated contracting states

Designated state(s): BE DE FR GB NL SE

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

Designated state(s): BE DE FR GB NL SE

17P Request for examination filed

Effective date: 19861127

17Q First examination report despatched

Effective date: 19871015

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE FR GB NL SE

REF Corresponds to:

Ref document number: 3570453

Country of ref document: DE

Date of ref document: 19890629

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19891231

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19900122

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19900125

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19900213

Year of fee payment: 6

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19900801

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19901129

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19910107

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19910108

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19910131

GBPC Gb: european patent ceased through non-payment of renewal fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19911001

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19920930

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

EUG Se: european patent has lapsed

Ref document number: 85400018.9

Effective date: 19910910