EP0417233B1 - Process for operating a coal-based fluidized bed combustor and fluidized bed combustor - Google Patents

Process for operating a coal-based fluidized bed combustor and fluidized bed combustor Download PDF

Info

Publication number
EP0417233B1
EP0417233B1 EP90904768A EP90904768A EP0417233B1 EP 0417233 B1 EP0417233 B1 EP 0417233B1 EP 90904768 A EP90904768 A EP 90904768A EP 90904768 A EP90904768 A EP 90904768A EP 0417233 B1 EP0417233 B1 EP 0417233B1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
bed
coal
bed material
ash
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
EP90904768A
Other languages
German (de)
French (fr)
Other versions
EP0417233A1 (en
Inventor
Gerhard Scholl
Hans-Karl Petzel
Lothar Stadie
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.)
Saarbergwerke AG
Siemens AG
Original Assignee
Saarbergwerke AG
Siemens AG
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 Saarbergwerke AG, Siemens AG filed Critical Saarbergwerke AG
Publication of EP0417233A1 publication Critical patent/EP0417233A1/en
Application granted granted Critical
Publication of EP0417233B1 publication Critical patent/EP0417233B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/24—Devices for removal of material from the bed
    • F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts

Definitions

  • the invention relates to a method for operating a coal-based fluidized-bed furnace, in which comminuted coal is fed to a fluidized bed and burned with the bed material.
  • the invention further relates to a system for fluidized bed firing with a conveyor line for the supply of coal and with a nozzle base on which a fluidized bed consisting of bed material is stored during operation.
  • Coal that is ground to the size of the fluidized bed is used to operate a fluidized bed furnace. It is introduced into the fluidized bed, usually via the free space arranged above the fluidized bed. Then it is burned in a homogeneous mixture with the bed material.
  • This bed material is made up of sand and ash particles, that have previously reached the fluidized bed with the coal, but are also formed by migrating coal particles.
  • the fluidized bed is continuously depleted of fine-grained bed material.
  • the coarse-grained fractions increase continuously and settle on the nozzle bottom of the fluidized bed over a long period of operation. This in turn leads to clogging of individual nozzles for the supply of carrier air.
  • the result of this is that locally different zones with little or no air throughput and zones with increased air throughput arise.
  • the temperature homogeneity of the fluidized bed which is necessary for the decoupling of the heat generated, for example via a heat exchanger system, is thereby substantially disturbed.
  • temperature streaks form over the areas with increased air throughput in the free space of the fluidized bed furnace.
  • the invention is based on the object of specifying a method of the type mentioned at the outset which makes it possible to operate a coal-based fluidized-bed furnace without problems even over a relatively long period of time. Furthermore, a system for fluidized bed firing of the type mentioned at the beginning is to be specified, in which the formation of slag can be avoided over a longer period of time.
  • the first-mentioned object is achieved in that part of the bed material from the lower region of the fluidized bed drawn off continuously or discontinuously, then preferably cooled, then processed to a predetermined maximum fluidized bed-specific grain size and then returned to the fluidized bed.
  • the proposal according to the invention aims to no longer set the optimum grain size band of the bed material of a fluidized bed firing system by grinding the fresh coal supplied, but instead to enable this by (preferably continuous) refurbishment of the bed material.
  • the bed material can be worked up in a simple manner by means of a sieving device which is set to the required grain width band and which thus separates a fine-grain fraction and a coarse-grain fraction.
  • the coarse-grain fraction that does not pass the sieving device is preferably ground in a comminution device or, in particular, in a grinding device and fed back to the sieving device in comminuted form.
  • a wind sifting can also be carried out instead of the screening.
  • the predetermined maximum grain size can be, for example, 3 to 4 mm.
  • the setting of the optimum fluidized bed grain size band no longer takes place via the coal supplied, only a relatively coarse grinding of the coal supplied and fed to the fluidized bed is required.
  • the use of the coarse-grained coal has the further advantage that the free surface of the supplied coal is relatively small overall compared to a finely ground coal.
  • a further reduction in the outgassing of the fresh fuel (coal) in the free space above the fluidized bed can be achieved in that, according to a development of the invention, the prepared and recycled bed material (ash) is not introduced into the fluidized bed separately from the fuel (coal), but instead is previously mixed with this fuel.
  • the proportion of cold inert material increases when the coal is fed in, as a result of which a decrease in temperature in the free space is achieved during the fuel input.
  • the coarse-grained fraction of the coal slowly migrates to the bottom of the fluidized bed. It is - as explained - subtracted and then processed.
  • an amount of bed material ie predominantly ash
  • the deduction for excess bed material can in principle be arranged on the nozzle base or in front of the screening device. Prefers but it is provided that the deduction for excess bed material is arranged in the transport path behind the device for processing the bed material. This is advantageous if the material removed here is temporarily stored in a bunker and then processed further. It is then already prepared for further processing in the fluidized bed.
  • the invention makes it possible to burn coals with different calorific values in a system for fluidized bed firing without great demands on the preparation and grinding.
  • the figure shows a boiler 1 operated with a coal-based fluidized bed firing with a fluidized bed 20, the upper level of which is indicated by an arrow 2.
  • the carrier air 1 for the fluidized bed 20 is fed to an air box 30 through a line 3. From there, it is introduced into the bed material of the fluidized bed 20 via distributor nozzles 4, which are arranged in a nozzle bottom 9.
  • this bed 20 is a mixture of coal particles and particles of coal-based ash, that is to say coal and burned and unburned residues.
  • the heat generated in the fluidized bed 20 is here decoupled indirectly via a heat exchanger system 5 located above the nozzle base 9, for example with the aid of air or water as the heat exchange medium.
  • the heat can be used to heat the working medium of a gas or steam turbine, not shown here.
  • the fluidized bed 20 has a temperature of 850 ° C., for example. It is important that during operation the temperature distribution is as uniform as possible everywhere in the fluidized bed 20, so that no slag can form from ash and carbon particles which settles in the boiler 1 and / or in the flue gas flue.
  • Those loaded with fine dust or fine bag Flue gases g from the furnace first pass through a space 6 provided above the fluidized bed 20. They are then fed, for example at 950 ° C., via a fume cupboard 7 to devices for dust and pollutant separation, not shown here. From there they get into a heat exchanger (not shown), for example a steam generator.
  • Crushed, but relatively coarse-grained (coarsely ground) fresh coal k is introduced into the free space 6 via a conveyor path 8 above the fluidized bed level 2, for example by means of a distributor or a centrifuge (not shown). Instead, the introduction could also be made in the area of the fluidized bed 20, for example by blowing or other known techniques.
  • the above-mentioned mixing of the larger and smaller particles present occurs due to the air blowing. Due to the vertical migration and gravity, the coarser particles will predominantly be located in the lower part of the fluidized bed.
  • the bed material a that accumulates in the area of the nozzle base 9 of the fluidized bed 20 is drawn off via a discharge device, in the present case via a discharge opening 9a arranged in the nozzle base 9 and by means of an ash or cellular wheel sluice 10. For reasons of redundancy, several such discharge devices 9a, 10 can also be present.
  • the withdrawal is preferably carried out continuously.
  • the stripped bed material a essentially ash, is then cooled, for example by natural cooling when left lying or - as in the present case - by forced cooling in an ash cooler 11.
  • the bed material a which has been drawn off and then cooled and comprises all possible particle or grain sizes is then fed to a device 12, 13 for processing to a predetermined maximum fluidized bed-specific grain size.
  • the maximum grain size that can be further processed can be, for example, 4 mm.
  • Another grain size can of course also be specified; this depends on the operating parameters that are available or should be set.
  • the processing device comprises a sieve device 12, a comminution device 13, for example an ash breaker, and a transport line 14.
  • the sieve device 12 separates a fine grain fraction a ', in the example with a grain size below 4 mm, and a coarse grain fraction A', in the example with a grain size of more than 4 mm.
  • the coarse grain fraction A ' is fed to the comminution device 13. Its output is connected via line 14 to the input of the screening device 12.
  • the coarse-grain fraction A ′ which does not pass through the screening device 12 is drawn off, comminuted in the ash crusher 13 and then fed again to the screening device 12 via the line 14.
  • the amount of bed material a 'drawn off and processed per unit of time is preferably greater than the amount of ash contained in the coal k supplied per unit of time.
  • the bed material a 'prepared in accordance with the required grain size is transported into the fluidized bed 20 by suitable conveying means. In the present case, this is done by means of a conveyor 15 on a conveyor path 18, for example a conveyor belt. Pneumatic conveying is also possible.
  • the bed material a ' is preferably mixed with fresh coal k in a mixing space 19 in the conveyor section 8.
  • the processed material a ' is guided together with this coal k through the free space 6 into the fluidized bed 20.
  • the material a 'can also be thrown onto the fluidized bed 20 separately from the coal k, as shown.
  • Excess material a ′′ is drawn off the system via an ash extraction or an ash lock 16 behind the screening device 12.
  • This ash lock 16 is preferably designed to be adjustable; for example, it can be adjusted by means of a motor.
  • the deduction takes place - taking into account ash content and promotion of the coal k and the discharge speed at the lock 10 - so that the level 2 of the fluidized bed 20 is kept at a constant level.
  • the extracted material a '' is stored in a sand or ash bunker. It can possibly be reused, that is to say the coal k in the mixing chamber 19 can be supplied later.
  • the ash lock 16 can also be arranged at another location, for example for the removal of unprocessed bed material a in front of the screening device 12. However, at this point it has the advantage that material a ′′ of the correct maximum grain size for later reuse provided.
  • the preparation described ensures that the required grain size range 0 to, for example, 4 mm for the bed material can be approximately maintained within the fluidized bed 20.
  • a relatively coarse-grained coal k can be used, which saves preparation and grinding costs.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Greenhouses (AREA)
  • Absorbent Articles And Supports Therefor (AREA)

Abstract

PCT No. PCT/DE90/00254 Sec. 371 Date Dec. 12, 1990 Sec. 102(e) Date Dec. 12, 1990 PCT Filed Mar. 30, 1990 PCT Pub. No. WO90/12246 PCT Pub. Date Oct. 18, 1990.Some part (a) of the bed material is withdrawn continuously (9e, 10) from the lower region of the fluidized bed (20), cooled (11), screened (12, 13) on a belt (a') to obtain a particle size specific to the fluidized bed, and then recycled to the fluidized bed (15, 18).

Description

Die Erfindung betrifft ein Verfahren zum Betreiben einer Anlage zur Wirbelbettfeuerung auf Kohlebasis, bei dem zerkleinerte Kohle einem Wirbelbett zugeführt und mit dem Bettmaterial verbrannt wird. Die Erfindung betrifft weiter eine Anlage zur Wirbelbettfeuerung mit einer Förderstrecke zur Zuführung von Kohle und mit einem Düsenboden, auf dem im Betrieb ein aus Bettmaterial bestehendes Wirbelbett lagert.The invention relates to a method for operating a coal-based fluidized-bed furnace, in which comminuted coal is fed to a fluidized bed and burned with the bed material. The invention further relates to a system for fluidized bed firing with a conveyor line for the supply of coal and with a nozzle base on which a fluidized bed consisting of bed material is stored during operation.

Es ist bekannter Stand der Technik, Kohle zur Dampf- und/oder Elektrizitätserzeugung in Anlagen zur Wirbelbettfeuerung zu verbrennen (Siemens-Energietechnik 2 (1980), Heft 7, Seiten 231 bis 235 oder Dokument GB-A-2 124 101). Dabei ergeben sich zwei wesentliche Vorteile. Zum einen erfolgt die Verbrennung im Wirbelbett bei relativ niedrigen Temperaturen, so daß im Vergleich zu den bekannten Feuerungen mit Trocken- oder gar Naßentaschung die Stickoxidbildung relativ gering ist. Zum anderen stellt die Verbrennung im Wirbelbett verhältnismäßig geringe Anforderungen an die Qualität der eingesetzten Kohle, das heißt, es kann auch eine vergleichsweise grob aufgemahlene Kohle mit hohem Aschegehalt ohne weiteres verbrannt werden. Unter "Asche" sind dabei die in der Kohle enthaltenen, nicht brennbaren Substanzen wie Sand, Lehm, Salze, Metallverbindungen und ähnliches zu verstehen.It is known prior art to burn coal for generating steam and / or electricity in fluidized bed combustion plants (Siemens-Energietechnik 2 (1980), No. 7, pages 231 to 235 or document GB-A-2 124 101). This has two major advantages. On the one hand, the combustion takes place in the fluidized bed at relatively low temperatures, so that the nitrogen oxide formation is relatively low compared to the known furnaces with dry or even wet ash removal. On the other hand, combustion in a fluidized bed places relatively low demands on the quality of the coal used, which means that a comparatively coarsely ground coal with a high ash content can also be burned without further notice. "Ash" is to be understood as the non-combustible substances contained in the coal, such as sand, clay, salts, metal compounds and the like.

Beim Betrieb einer Anlage zur Wirbelbettfeuerung wird Kohle eingesetzt, die auf die wirbelbettspezifische Korngröße aufgemahlen ist. Sie wird in das Wirbelbett eingeleitet, und zwar meist über den oberhalb des Wirbelbetts angeordneten Freiraum. Sodann wird sie in homogener Mischung mit dem Bettmaterial verbrannt. Dieses Bettmaterial wird durch Sand- und Aschepartikel, die zuvor mit der Kohle in das Wirbelbett gelangt sind, aber auch durch wandernde Kohlepartikel gebildet.Coal that is ground to the size of the fluidized bed is used to operate a fluidized bed furnace. It is introduced into the fluidized bed, usually via the free space arranged above the fluidized bed. Then it is burned in a homogeneous mixture with the bed material. This bed material is made up of sand and ash particles, that have previously reached the fluidized bed with the coal, but are also formed by migrating coal particles.

Als nachteilig hat es sich dabei erwiesen, daß insbesondere bei diskontinuierlichem Ascheabzug aufgrund des Flugstaubaustrages mit dem Rauchgas kontinuierlich eine Verarmung des Wirbelbettes an feinkörnigem Bettmaterial erfolgt. Die Grobkornanteile nehmen ständig zu und setzen sich bei längerer Betriebszeit auf dem Düsenboden des Wirbelbettes ab. Dies wiederum führt zur Verstopfung einzelner Düsen für die Zufuhr der Trägerluft. Dies hat zur Folge, daß örtlich verschieden Zonen mit wenig oder überhaupt keinem Luftdurchsatz sowie Zonen mit erhöhtem Luftdurchsatz entstehen. Damit wird die Temperaturhomogenität des Wirbelbettes, die für die Auskopplung der erzeugten Wärme beispielsweise über ein Wärmetauschersystem erforderlich ist, wesentlich gestört. Hinzu kommt, daß sich über den Bereichen mit erhöhtem Luftdurchsatz im Freiraum der Anlage zur Wirbelschichtfeuerung Temperatursträhnen bilden. Dies sind dünne langgestreckte Getriebe mit Temperaturen, die über dem Ascheerweichungspunkt liegen. Als Folge davon kommt es zu Verschlackungen des Freiraums, zum Beispiel in Form von Nestern. Diese Verschlackungen können zum Abstellen der Anlage zur Wirbelschichtfeuerung zwingen. Wichtig ist also eine möglichst gleichmäßige Temperaturverteilung über das gesamte Wirbelbett, damit keine Schlackeablagerungen entstehen können.It has proven to be disadvantageous that, in particular in the case of discontinuous ash extraction due to the discharge of fly dust with the flue gas, the fluidized bed is continuously depleted of fine-grained bed material. The coarse-grained fractions increase continuously and settle on the nozzle bottom of the fluidized bed over a long period of operation. This in turn leads to clogging of individual nozzles for the supply of carrier air. The result of this is that locally different zones with little or no air throughput and zones with increased air throughput arise. The temperature homogeneity of the fluidized bed, which is necessary for the decoupling of the heat generated, for example via a heat exchanger system, is thereby substantially disturbed. In addition, temperature streaks form over the areas with increased air throughput in the free space of the fluidized bed furnace. These are thin, elongated gears with temperatures above the ash softening point. As a result, there is slagging of the open space, for example in the form of nests. This slagging can force the system to shut down the fluidized bed furnace. It is therefore important that the temperature is distributed as evenly as possible over the entire fluidized bed, so that no slag deposits can form.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art anzugeben, das es ermöglicht, eine Anlage zur Wirbelbettfeuerung auf Kohlebasis auch über einen längeren Zeitraum problemlos zu betreiben. Weiterhin soll eine Anlage zur Wirbelbettfeuerung der eingangs genannten Art angegeben werden, bei der die Bildung von Schlacke über einen längeren Zeitraum vermieden werden kann.The invention is based on the object of specifying a method of the type mentioned at the outset which makes it possible to operate a coal-based fluidized-bed furnace without problems even over a relatively long period of time. Furthermore, a system for fluidized bed firing of the type mentioned at the beginning is to be specified, in which the formation of slag can be avoided over a longer period of time.

Die erstgenannte Aufgabe wird erfindungsgemäß dadurch gelöst, daß ein Teil des Bettmaterials aus dem unteren Bereich des Wirbelbettes kontinuierlich oder diskontinuierlich abgezogen, danach vorzugsweise gekühlt, dann bis zu einer vorgegebenen maximalen wirbelbettspezifischen Korngröße aufbereitet und sodann in das Wirbelbett zurückgeführt wird.The first-mentioned object is achieved in that part of the bed material from the lower region of the fluidized bed drawn off continuously or discontinuously, then preferably cooled, then processed to a predetermined maximum fluidized bed-specific grain size and then returned to the fluidized bed.

Die zweitgenannte Aufgabe wird erfindungsgemäß gelöst durch eine Anlage, die gekennzeichnet ist durch

  • a) eine Austragseinrichtung für das Abziehen eines Teils des Bettmaterials, das sich im unteren Teil des Wirbelbetts befindet,
  • b) vorzugsweise einen der Austragseinrichtung nachgeschalteten Aschekühler zur Abkühlung des abgezogenen Bettmaterials,
  • c) eine Einrichtung zur Aufbereitung des Bettmaterials auf eine vorgegebene maximale Wirbelbettspezifische Korngröße,
  • d) einen Abzug für überschüssiges Bettmaterial und
  • e) Fördermittel zum Transport des aufbereiteten Bettmaterials in das Wirbelbett.
The second object is achieved according to the invention by a system which is characterized by
  • a) a discharge device for pulling off part of the bed material located in the lower part of the fluidized bed,
  • b) preferably an ash cooler connected downstream of the discharge device for cooling the bed material taken off,
  • c) a device for processing the bed material to a predetermined maximum fluid bed-specific grain size,
  • d) a deduction for excess bed material and
  • e) Funding for transporting the prepared bed material into the fluidized bed.

Der erfindungsgemäße Vorschlag zielt darauf ab, das optimale Korngrößenband des Bettmaterials einer Anlage zur Wirbelschichtfeuerung nicht mehr wie bisher über die Aufmahlung der zugeführten Frischkohle einzustellen, sondern dies durch (bevorzugt kontinuierliche) Aufarbeitung des Bettmaterials zu ermöglichen.The proposal according to the invention aims to no longer set the optimum grain size band of the bed material of a fluidized bed firing system by grinding the fresh coal supplied, but instead to enable this by (preferably continuous) refurbishment of the bed material.

Die Aufarbeitung des Bettmaterials kann dabei in einfacher Weise mittels einer Siebeinrichtung erfolgen, die auf das benötigte Kornbreitenband eingestellt ist und die somit eine Feinkornfraktion und eine Grobkornfraktion abscheidet. Dabei wird bevorzugt die die Siebeinrichtung nicht passierende Grobkornfraktion in einer Zerkleinerungs- oder speziell in einer Mahleinrichtung aufgemahlen und in zerkleinerter Form erneut der Siebeinrichtung zugeführt. Anstelle der Siebung kann prinzipiell auch eine Windsichtung durchgeführt werden. Die vorgegebene maximale Korngröße kann zum Beispiel 3 bis 4 mm betragen.The bed material can be worked up in a simple manner by means of a sieving device which is set to the required grain width band and which thus separates a fine-grain fraction and a coarse-grain fraction. In this case, the coarse-grain fraction that does not pass the sieving device is preferably ground in a comminution device or, in particular, in a grinding device and fed back to the sieving device in comminuted form. In principle, a wind sifting can also be carried out instead of the screening. The predetermined maximum grain size can be, for example, 3 to 4 mm.

Da gemäß der Erfindung die Einstellung dis optimalen Wirbelbett-Korngrößenbandes nicht mehr über die zugeführte Kohle erfolgt, ist nur noch eine relativ grobe Aufmahlung der angelieferten, dem Wirbelbett zugeführten Kohle erforderlich. Neben der Einsparung an Aufbereitungs- und Mahlkosten für die Kohle bringt die Verwendung der grobkörnigen Kohle den weiteren Vorteil, daß im Vergleich zu einer feinaufgemahlenen Kohle die freie Oberfläche der zugeführten Kohle insgesamt relativ klein ist. Dadurch gast - bei Kohleeintrag in den Freiraum oberhalb des Wirbelbettes - nur ein geringer Teil der Kohle bereits während des Eintrages in diesem Freiraum aus. Folglich bleibt die Freiraumtemperatur relativ niedrig, so daß Probleme hinsichtlich verstärkter Schlackebildung nicht mehr auftreten.Since, according to the invention, the setting of the optimum fluidized bed grain size band no longer takes place via the coal supplied, only a relatively coarse grinding of the coal supplied and fed to the fluidized bed is required. In addition to saving processing and grinding costs for the coal, the use of the coarse-grained coal has the further advantage that the free surface of the supplied coal is relatively small overall compared to a finely ground coal. As a result, when coal is being fed into the free space above the fluidized bed, only a small part of the coal is already outgassing during the entry into this free space. As a result, the free space temperature remains relatively low, so that problems with increased slag formation no longer occur.

Eine weitere Verringerung der Ausgasung des frischen Brennstoffes (Kohle) im Freiraum oberhalb dem Wirbelbett läßt sich dadurch erreichen, daß nach einer Weiterbildung der Erfindung das aufbereitete und zurückgeführte Bettmaterial (Asche) nicht getrennt von dem Brennstoff (Kohle) in das Wirbelbett eingeleitet wird, sondern vorher mit diesem Brennstoff vermischt wird. Dadurch steigt der Anteil an kaltem Inertmaterial (Asche, Sand, etc.) bei der Zuführung der Kohle, wodurch während des Brennstoffeintrages eine Temperaturabsenkung im Freiraum erreicht wird.A further reduction in the outgassing of the fresh fuel (coal) in the free space above the fluidized bed can be achieved in that, according to a development of the invention, the prepared and recycled bed material (ash) is not introduced into the fluidized bed separately from the fuel (coal), but instead is previously mixed with this fuel. As a result, the proportion of cold inert material (ash, sand, etc.) increases when the coal is fed in, as a result of which a decrease in temperature in the free space is achieved during the fuel input.

Im Zuge der Verbrennung wandert der Grobkornanteil der Kohle langsam bis zum Düsenboden des Wirbelbettes. Er wird hier - wie erläutert - abgezogen und sodann aufbereitet. Zweckmäßigerweise wird dabei pro Zeiteinheit immer eine Menge an Bettmaterial (also vorwiegend Asche) abgezogen, die größer ist als die Menge, die als Grobkorn über die Kohle dem Wirbelbett zugeführt wird. Auf diese Weise wird ein Absetzen des Grobkorns auf dem Wirbelbett-Düsenboden mit Sicherheit vermieden.During the course of the combustion, the coarse-grained fraction of the coal slowly migrates to the bottom of the fluidized bed. It is - as explained - subtracted and then processed. Advantageously, an amount of bed material (ie predominantly ash) is always deducted per unit of time, which is greater than the amount that is fed to the fluidized bed as coarse grain via the coal. In this way, a deposit of the coarse grain on the fluidized bed nozzle bottom is avoided with certainty.

Der Abzug für überschüssiges Bettmaterial kann prinzipiell am Düsenboden oder vor der Siebeinrichtung angeordnet sein. Bevorzugt ist aber vorgesehen, daß der Abzug für überschüssiges Bettmaterial im Transportweg hinter der Einrichtung zur Aufbereitung des Bettmaterials angeordnet ist. Dies ist von Vorteil, wenn das hier abgezogene Material in einem Bunker zwischengelagert und dann weiterverarbeitet wird. Es ist dann für die Weiterverarbeitung im Wirbelbett bereits aufbereitet.The deduction for excess bed material can in principle be arranged on the nozzle base or in front of the screening device. Prefers but it is provided that the deduction for excess bed material is arranged in the transport path behind the device for processing the bed material. This is advantageous if the material removed here is temporarily stored in a bunker and then processed further. It is then already prepared for further processing in the fluidized bed.

Insgesamt ermöglicht es die Erfindung, in einer Anlage zur Wirbelbettfeuerung problemlos Kohlen mit unterschiedlichem Heizwert ohne große Anforderungen an die Aufbereitung und Aufmahlung zu verbrennen.Overall, the invention makes it possible to burn coals with different calorific values in a system for fluidized bed firing without great demands on the preparation and grinding.

Die Erfindung und weitere Ausgestaltungen werden im folgenden anhand des in der Figur schematisch dargestellten Ausführungsbeispiels einer Anlage zur Wirbelbettfeuerung näher erläutert.The invention and further refinements are explained in more detail below with reference to the exemplary embodiment of a system for fluidized bed firing, which is shown schematically in the figure.

Die Figur zeigt einen mit einer Wirbelbettfeuerung auf Kohlebasis betriebenen Kessel 1 mit einem Wirbelbett 20, dessen oberes Niveau durch einen Pfeil 2 gekennzeichnet ist. Die Trägerluft 1 für das Wirbelbett 20 wird durch eine Leitung 3 einem Luftkasten 30 zugeführt. Sie wird von dort über Verteilerdüsen 4, die in einem Düsenboden 9 angeordnet sind, in das bettmaterial des Wirbelbettes 20 eingeleitet. Im vorliegenden Fall ist dies Bett 20 eine Mischung aus Kohlepartikeln und Partikeln von kohlestämmiger Asche, also aus Kohle und verbrannten und nicht-verbrannten Rückständen. Die im Wirbelbett 20 erzeugte Wärme wird hier indirekt über ein über dem Düsenboden 9 befindliches Wärmetauschersystem 5 ausgekoppelt, zum Beispiel mit Hilfe von Luft oder Wasser als Wärmetauschmedium. Die Wärme kann zur Erhitzung des Arbeitsmittels einer hier nicht dargestellten Gas- oder Dampfturbine verwendet werden. Im Betrieb hat das Wirbelbett 20 beispielsweise eine Temperatur von 850 °C. Wichtig ist, daß sich im Betrieb eine möglichst gleichmäßige Temperaturverteilung überall im Wirbelbett 20 einstellt, damit sich aus Asche- und Kohlepartikeln keine Schlacke bilden kann, die sich im Kessel 1 und/oder im Rauchgaszug absetzt. Die mit Feinstaub oder Feinstasche beladenen Rauchgase g aus der Feuerung passieren zunächst einen oberhalb des Wirbelbettes 20 vorgesehenen Freiraum 6. Sie werden dann, zum Beispiel mit 950 °C, über einen Abzug 7 hier nicht dargestellten Einrichtungen zur Staub- und Schadstoffabtrennung zugeführt. Von dort gelangen sie in einen (nicht gezeigten) Wärmetauscher, zum Beispiel in einen Dampferzeuger.The figure shows a boiler 1 operated with a coal-based fluidized bed firing with a fluidized bed 20, the upper level of which is indicated by an arrow 2. The carrier air 1 for the fluidized bed 20 is fed to an air box 30 through a line 3. From there, it is introduced into the bed material of the fluidized bed 20 via distributor nozzles 4, which are arranged in a nozzle bottom 9. In the present case, this bed 20 is a mixture of coal particles and particles of coal-based ash, that is to say coal and burned and unburned residues. The heat generated in the fluidized bed 20 is here decoupled indirectly via a heat exchanger system 5 located above the nozzle base 9, for example with the aid of air or water as the heat exchange medium. The heat can be used to heat the working medium of a gas or steam turbine, not shown here. In operation, the fluidized bed 20 has a temperature of 850 ° C., for example. It is important that during operation the temperature distribution is as uniform as possible everywhere in the fluidized bed 20, so that no slag can form from ash and carbon particles which settles in the boiler 1 and / or in the flue gas flue. Those loaded with fine dust or fine bag Flue gases g from the furnace first pass through a space 6 provided above the fluidized bed 20. They are then fed, for example at 950 ° C., via a fume cupboard 7 to devices for dust and pollutant separation, not shown here. From there they get into a heat exchanger (not shown), for example a steam generator.

Zerkleinerte, aber relativ grobkörnige (grob aufgemahlene) Frischkohle k wird über eine Förderstrecke 8 oberhalb des Wirbelbettniveaus 2 in den Freiraum 6 eingeführt, zum Beispiel mittels eines Zuteilers oder einer Schleuder (nicht gezeigt). Die Einführung könnte stattdessen auch im Bereich des Wirbelbetts 20 vorgenommen werden, zum Beispiel durch Einblasen oder andere bekannte Techniken.Crushed, but relatively coarse-grained (coarsely ground) fresh coal k is introduced into the free space 6 via a conveyor path 8 above the fluidized bed level 2, for example by means of a distributor or a centrifuge (not shown). Instead, the introduction could also be made in the area of the fluidized bed 20, for example by blowing or other known techniques.

Im Wirbelbett 20 stellt sich durch das Lufteinblasen die genannte Vermischung der vorhandenen größeren und kleineren Partikel ein. Bedingt durch die Vertikalwanderung und die Schwerkraft werden sich aber im unteren Teil des Wirbelbettes überwiegend die gröberen Partikel befinden.In the fluidized bed 20, the above-mentioned mixing of the larger and smaller particles present occurs due to the air blowing. Due to the vertical migration and gravity, the coarser particles will predominantly be located in the lower part of the fluidized bed.

Das im Bereich des Düsenbodens 9 des Wirbelbettes 20 sich ansammelnde Bettmaterial a wird über eine Austragseinrichtung, vorliegend über eine im Düsenboden 9 angeordnete Abzugsöffnung 9a und mittels einer Asche- oder Zellenradschleuse 10, abgezogen. Aus Redundanzgründen können auch mehrere solche Austragseinrichtungen 9a, 10 vorhanden sein. Der Abzug erfolgt bevorzugt kontinuierlich. Das abgezogene Bettmaterial a, im wesentlichen Asche, wird sodann abgekühlt, zum Beispiel durch Naturkühlung beim Liegenlassen oder - wie vorliegend - durch Zwangskühlung in einem Aschekühler 11.The bed material a that accumulates in the area of the nozzle base 9 of the fluidized bed 20 is drawn off via a discharge device, in the present case via a discharge opening 9a arranged in the nozzle base 9 and by means of an ash or cellular wheel sluice 10. For reasons of redundancy, several such discharge devices 9a, 10 can also be present. The withdrawal is preferably carried out continuously. The stripped bed material a, essentially ash, is then cooled, for example by natural cooling when left lying or - as in the present case - by forced cooling in an ash cooler 11.

Das abgezogene und sodann abgekühlte Bettmaterial a, das alle möglichen Partikel- oder Korngrößen umfaßt, wird sodann einer Einrichtung 12, 13 zur Aufbereitung auf eine Vorgegebene maximale wirbelbettspezifische Korngröße zugeführt. Diese vorgegebene maximale Korngröße, die weiterverarbeitet werden darf, kann zum Beispiel 4 mm betragen. Natürlich kann auch eine andere Korngröße vorgegeben werden; das richtet sich nach den Betriebsparametern, die vorhanden sind oder eingestellt werden sollen. Vorliegend umfaßt die Aufbereitungseinrichtung eine Siebeinrichtung 12, eine Zerkleinerungseinrichtung 13, zum Beispiel einen Aschebrecher, und eine Transportleitung 14. Die Siebeinrichtung 12 scheidet eine Feinkornfraktion a', und zwar im Beispiel mit einer Körnung unter 4 mm, und eine Grobkornfraktion A', im Beispiel mit einer Körnung über 4 mm, ab. Die Grobkornfraktion A' wird der Zerkleinerungseinrichtung 13 zugeleitet. Deren Ausgang ist über die Leitung 14 an den Eingang der Siebeinrichtung 12 angeschlossen. Im Zuge der Aufbereitung wird die nicht die Siebeinrichtung 12 passierende Grobkornfraktion A' abgezogen, in dem Aschebrecher 13 zerkleinert und dann über die Leitung 14 erneut der Siebeinrichtung 12 zugeführt. Vorzugsweise ist die pro Zeiteinheit abgezogene und aufbereitete Menge an Bettmaterial a' größer als die pro Zeiteinheit mit der Kohle k zugeführte, in dieser enthaltene Aschemenge.The bed material a which has been drawn off and then cooled and comprises all possible particle or grain sizes is then fed to a device 12, 13 for processing to a predetermined maximum fluidized bed-specific grain size. This given The maximum grain size that can be further processed can be, for example, 4 mm. Another grain size can of course also be specified; this depends on the operating parameters that are available or should be set. In the present case, the processing device comprises a sieve device 12, a comminution device 13, for example an ash breaker, and a transport line 14. The sieve device 12 separates a fine grain fraction a ', in the example with a grain size below 4 mm, and a coarse grain fraction A', in the example with a grain size of more than 4 mm. The coarse grain fraction A 'is fed to the comminution device 13. Its output is connected via line 14 to the input of the screening device 12. In the course of the processing, the coarse-grain fraction A ′ which does not pass through the screening device 12 is drawn off, comminuted in the ash crusher 13 and then fed again to the screening device 12 via the line 14. The amount of bed material a 'drawn off and processed per unit of time is preferably greater than the amount of ash contained in the coal k supplied per unit of time.

Das entsprechend der geforderten Korngröße aufbereitete Bettmaterial a' wird durch geeignete Fördermittel in das Wirbelbett 20 transportiert. Vorliegend geschieht dies mittels eines Förderorgans 15 auf einem Förderweg 18, zum Beispiel einem Transportband. Auch eine pneumatische Förderung ist möglich. Das Bettmaterial a' wird bevorzugt in einem Mischraum 19 in der Förderstrecke 8 mit Frischkohle k vermischt. Das aufbereitete Material a' wird zusammen mit dieser Kohle k über den Freiraum 6 in das Wirbelbett 20 geführt. Natürlich kann das Material a' auch - wie eingezeichnet - getrennt von der Kohle k auf das Wirbelbett 20 geworfen werden.The bed material a 'prepared in accordance with the required grain size is transported into the fluidized bed 20 by suitable conveying means. In the present case, this is done by means of a conveyor 15 on a conveyor path 18, for example a conveyor belt. Pneumatic conveying is also possible. The bed material a 'is preferably mixed with fresh coal k in a mixing space 19 in the conveyor section 8. The processed material a 'is guided together with this coal k through the free space 6 into the fluidized bed 20. Of course, the material a 'can also be thrown onto the fluidized bed 20 separately from the coal k, as shown.

Überschüssiges Material a'' wird über einen Ascheabzug oder eine Ascheschleuse 16 hinter der Siebeinrichtung 12 aus der Anlage abgezogen. Diese Ascheschleuse 16 ist bevorzugt regelbar ausgeführt; sie ist zum Beispiel mittels eines Motors verstellbar.Excess material a ″ is drawn off the system via an ash extraction or an ash lock 16 behind the screening device 12. This ash lock 16 is preferably designed to be adjustable; for example, it can be adjusted by means of a motor.

Der Abzug geschieht - unter Berücksichtigung von Aschegehalt und Förderung der Kohle k sowie der Austragsgeschwindigkeit an der Schleuse 10 - so, daß das Niveau 2 des Wirbelbettes 20 auf konstanter Höhe gehalten wird. Das abgezogene Material a'' wird in einem Sand- oder Aschebunker gespeichert. Es kann eventuell wiederverwendet, das heißt der Kohle k im Mischraum 19 später zugeführt werden. Die Ascheschleuse 16 kann auch an anderer Stelle angeordnet sein, zum Beispiel zum Abzug von nicht-aufbereitetem Bettmaterial a vor der Siebeinrichtung 12. An der vorliegenden Stelle hat sie jedoch den Vorteil, daß bereits Material a'' der richtigen maximalen Korngröße für die spätere Weiterverwendung bereitgestellt wird.The deduction takes place - taking into account ash content and promotion of the coal k and the discharge speed at the lock 10 - so that the level 2 of the fluidized bed 20 is kept at a constant level. The extracted material a '' is stored in a sand or ash bunker. It can possibly be reused, that is to say the coal k in the mixing chamber 19 can be supplied later. The ash lock 16 can also be arranged at another location, for example for the removal of unprocessed bed material a in front of the screening device 12. However, at this point it has the advantage that material a ″ of the correct maximum grain size for later reuse provided.

Aufgrund der beschriebenen Aufbereitung ist gewährleistet, daß innerhalb des Wirbelbettes 20 das geforderte Korngrößenband 0 bis zum Beispiel 4 mm für das Bettmaterial ständig in etwa eingehalten werden kann. An Aufbereitung und Mahlung der Frischkohle k selbst sind keine großen Anforderungen zu stellen. Es kann eine relativ grobkörnige Kohle k eingesetzt werden, wodurch Aufbereitungs- und Mahlkosten eingespart werden.The preparation described ensures that the required grain size range 0 to, for example, 4 mm for the bed material can be approximately maintained within the fluidized bed 20. There are no major requirements for the processing and grinding of the fresh coal k itself. A relatively coarse-grained coal k can be used, which saves preparation and grinding costs.

Claims (5)

  1. A method of operating a fluidized bed combustion apparatus based on coal, wherein coarsely ground unprocessed coal is conveyed to a fluidized bed and is burned mixed with the bed material and wherein a part of the bed material is discharged from the lower zone of the fluidized bed, is preferably cooled, is conveyed to a screening device, and the particles which pass through the screen are returned to the fluidized bed, characterised in that the oversize fraction produced in the screening device is ground and returned to the screening device.
  2. A method as claimed in Claim 1, characterised in that the recycled bed material is mixed with the coal before being conveyed to the fluidized bed.
  3. A method as claimed in one of Claims 1 or 2, characterised in that the quantity of bed material discharged and prepared per time unit is greater than the quantity of ash supplied with the coal and contained therein.
  4. A fluidized bed combustion apparatus comprising a nozzle plate (9) on which a fluidized bed (20) composed of bed material is mounted during operation, a discharging device (9a, 10) for discharging a part of the bed arterial (a) located in the lower zone of the fluidized bed (20), preferably an ash cooler (11) which is arranged downstream of the discharging device (9a, 10) and which serves to cool the discharged bed material (a), a device (12) for screening the bed arterial, and conveying means (15, 18) for transporting the screened bcd material (a') into the fluidized bed (20), characterised by a crushing device (13) which is assigned to the screening device (12, can be supplied with the oversize fraction (A') separated by the screening device (12) and the output of which is connected to the input of the screening device (12).
  5. An apparatus as claimed in Claim 4, characterised in that a mixing chamber (19) is provided in which the prepared bed material (a') can be mixed with the coal (k).
EP90904768A 1989-03-30 1990-03-30 Process for operating a coal-based fluidized bed combustor and fluidized bed combustor Expired - Lifetime EP0417233B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3910271A DE3910271A1 (en) 1989-03-30 1989-03-30 METHOD FOR OPERATING A CARBON-BASED COMBUSTION BED FIRING
DE3910271 1989-03-30

Publications (2)

Publication Number Publication Date
EP0417233A1 EP0417233A1 (en) 1991-03-20
EP0417233B1 true EP0417233B1 (en) 1993-06-09

Family

ID=6377455

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90904768A Expired - Lifetime EP0417233B1 (en) 1989-03-30 1990-03-30 Process for operating a coal-based fluidized bed combustor and fluidized bed combustor

Country Status (8)

Country Link
US (1) US5099801A (en)
EP (1) EP0417233B1 (en)
JP (1) JPH03505779A (en)
AT (1) ATE90436T1 (en)
DE (3) DE8916174U1 (en)
DK (1) DK0417233T3 (en)
ES (1) ES2042288T3 (en)
WO (1) WO1990012246A1 (en)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03213903A (en) * 1990-01-19 1991-09-19 Nkk Corp Burner for circulating fluidized-bed combustion with particle crusher
SE469043B (en) * 1991-09-05 1993-05-03 Abb Carbon Ab PROCEDURE AND DEVICE FOR HEATING OF BEDMASS IN PFBC PLANTS
SE9501886L (en) * 1995-05-19 1996-11-20 Nykomb Synergetics Technology Char and power generation systems and devices
EP1076206A1 (en) * 1999-08-13 2001-02-14 Ebara Corporation Method for processing furnace-bottom residue produced in gasification and slagging combustion furnace
US6554061B2 (en) * 2000-12-18 2003-04-29 Alstom (Switzerland) Ltd Recuperative and conductive heat transfer system
JP4570591B2 (en) * 2006-07-03 2010-10-27 中国電力株式会社 Method and system for reusing coarse particles recovered from fluidized bed boiler fuel production and supply equipment
DE102009013713A1 (en) * 2009-03-20 2010-09-23 Mvv Biopower Gmbh Method for operating a biomass cogeneration plant with a fluidized bed combustion
EP4206527A1 (en) * 2021-12-30 2023-07-05 Fescon Oy Method of operating a fluidized bed boiler and boiler plant

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE7413296L (en) * 1975-07-25 1975-10-30 Sprocket Properties Ltd COMBUSTION OVEN WITH PRESSURE GAS BED
DE2624302C2 (en) * 1976-05-31 1987-04-23 Metallgesellschaft Ag, 6000 Frankfurt Methods for carrying out exothermic processes
GB2007811B (en) * 1977-11-15 1982-03-03 Coal Industry Patents Ltd Fluised beds
US4227488A (en) * 1978-10-03 1980-10-14 Foster Wheeler Energy Corporation Fluidized bed unit including a cooling device for bed material
DE2929264A1 (en) * 1979-07-17 1981-01-29 Foster Wheeler Power Prod Fluidised bed combustor or reactor - passes combustion-supporting gas upwardly through bed of particulate material for entraining and separating outside housing
EP0028458B1 (en) * 1979-10-03 1985-04-03 Sandfire (Proprietary) Limited Fluidised-bed boilers
SE434087B (en) * 1981-02-19 1984-07-02 Stal Laval Turbin Ab INSTALLATION FOR COMBUSTION OF PURE SOLID FUEL IN A FIREBOARD WITH A FLUIDIZED BED
GB2124101A (en) * 1982-07-23 1984-02-15 Environment And Mechanical Ser Classification and recycling of fluidised bed material
US4505209A (en) * 1982-12-08 1985-03-19 Electrodyne Research Corporation Unfired drying and sorting apparatus for preparation of solid fuel
US4815418A (en) * 1987-03-23 1989-03-28 Ube Industries, Inc. Two fluidized bed type boiler
US4776288A (en) * 1987-07-31 1988-10-11 Metallgesellschaft Aktiengesellschaft Method for improving solids distribution in a circulating fluidized bed system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Chemical Engineering Progress, Vol. 80, No. 1, January 1984, (New York , US) W.R. Kelly et al:"Industrial application of fluidized-bed cogeneration system", pages 35-40, see page 39, figure 6 *

Also Published As

Publication number Publication date
ATE90436T1 (en) 1993-06-15
WO1990012246A1 (en) 1990-10-18
EP0417233A1 (en) 1991-03-20
JPH03505779A (en) 1991-12-12
DE8916174U1 (en) 1994-10-20
DE59001691D1 (en) 1993-07-15
ES2042288T3 (en) 1993-12-01
US5099801A (en) 1992-03-31
DK0417233T3 (en) 1993-11-01
DE3910271A1 (en) 1990-11-22

Similar Documents

Publication Publication Date Title
DE69133138T2 (en) TREATMENT OF FLYING BAGS BY CARBON BURNING OUT IN A DRY SPIRLED BULB
DE69634008T2 (en) DEVICE AND METHOD FOR CARBURETTING REMOVAL FROM AIRBAGS
EP0197577B1 (en) Method of cleaning contaminated soil
DE2627056A1 (en) Process for the production of cement clinkers
EP0579214B2 (en) Process for milling crude lignite
EP0302310A1 (en) Process and plant for the thermal disposal of waste
DE1809874B2 (en) Device for the dry distillation of bituminous or oil-containing, fine-grained materials for the purpose of obtaining liquid hydrocarbons
DE69508097T2 (en) PARTICULATE FUEL FROM WOOD WASTE, METHOD FOR PRODUCING THIS FUEL AND METHOD FOR GENERATING ENERGY WITH THIS FUEL
EP0417233B1 (en) Process for operating a coal-based fluidized bed combustor and fluidized bed combustor
WO2012028273A1 (en) Method and system for milling coal in inert operation or in non-inert operation
DE2732186A1 (en) METHOD AND APPARATUS FOR THE RECYCLING OF SOLIDS CONTAINING COMBUSTIBLE MATERIALS
DD141056A5 (en) METHOD AND DEVICE FOR THE PREPARATION AND COMBUSTION OF COAL
EP0526697B1 (en) Method and apparatus for treating mineral wool wastes
DE2943555C2 (en)
DE2325311A1 (en) CLINKER COOLING DEVICE
DE69429017T2 (en) PLANT FOR PRODUCING ASH-CONTAINING PRODUCTS AND ENERGY FROM WASTE
DE2333560A1 (en) SINTER PLANT FOR THE PRODUCTION OF SINTER FROM IRON ORES
DE1181360B (en) Process and system for waste incineration in a steam generator
DE69109269T2 (en) METHOD FOR SUPPLYING ABSORBENTS FOR COAL AND SULFUR TO A BURNER AND POWER PLANT IN WHICH THE METHOD APPLIES TO THE APPLICATION.
DE1783102B1 (en) Process for the treatment of coal-containing tailings
DE1571679C3 (en) Method and device for the joint production of coke dust and coke grits
DE19946517C2 (en) Process for crushing and drying moist fuel
DE10142290A1 (en) Treatment of residual waste, from household and similar waste, involves forming fraction by crushing, sieving and removing metals from waste, thermally drying to adjust residual moisture, and pressing to form pellets
DE202024000232U1 (en) Device for dry granulation of liquid slags resulting from fuel gasification and/or liquid ash separation from separators
DE1237511B (en) Method and device for processing and drying solid combustible material

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: 19901211

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE DE DK ES FR GB IT NL

17Q First examination report despatched

Effective date: 19920210

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE DE DK ES FR GB IT NL

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

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 19930609

Ref country code: NL

Effective date: 19930609

Ref country code: BE

Effective date: 19930609

REF Corresponds to:

Ref document number: 90436

Country of ref document: AT

Date of ref document: 19930615

Kind code of ref document: T

REF Corresponds to:

Ref document number: 59001691

Country of ref document: DE

Date of ref document: 19930715

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19930623

ET Fr: translation filed
REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2042288

Country of ref document: ES

Kind code of ref document: T3

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

Ref country code: AT

Payment date: 19960115

Year of fee payment: 7

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

Ref country code: DK

Payment date: 19960123

Year of fee payment: 7

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

Ref country code: GB

Payment date: 19960129

Year of fee payment: 7

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

Ref country code: ES

Payment date: 19960306

Year of fee payment: 7

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

Ref country code: FR

Payment date: 19960329

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: 19970330

Ref country code: DK

Effective date: 19970330

Ref country code: AT

Effective date: 19970330

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

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

Ref country code: ES

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 19970331

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19970330

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

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19971128

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 19990601

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

Ref country code: DE

Payment date: 20090312

Year of fee payment: 20

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

Ref country code: DE

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20100330