EP0126001B1 - Verfahren und Vorrichtung zur Behandlung eines Brennstoffes in einer Wirbelschicht - Google Patents

Verfahren und Vorrichtung zur Behandlung eines Brennstoffes in einer Wirbelschicht Download PDF

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Publication number
EP0126001B1
EP0126001B1 EP84400961A EP84400961A EP0126001B1 EP 0126001 B1 EP0126001 B1 EP 0126001B1 EP 84400961 A EP84400961 A EP 84400961A EP 84400961 A EP84400961 A EP 84400961A EP 0126001 B1 EP0126001 B1 EP 0126001B1
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EP
European Patent Office
Prior art keywords
temperature
zone
plant
fluidized bed
particles
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Expired
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EP84400961A
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English (en)
French (fr)
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EP0126001A1 (de
Inventor
Gérard Chrysostome
Robert Wang
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Creusot Loire SA
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Creusot Loire SA
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Priority to AT84400961T priority Critical patent/ATE32606T1/de
Publication of EP0126001A1 publication Critical patent/EP0126001A1/de
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Publication of EP0126001B1 publication Critical patent/EP0126001B1/de
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    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams

Definitions

  • the subject of the invention is an improved process and installation for treating a combustible material in a fluidized bed, applicable in particular to the gasification of coal.
  • a fluidized granular material treatment installation normally consists of a vertical reaction chamber supplied with granular combustible materials and provided at its base with means for injecting a fluidizing gas, the circulation speed of which can be adjusted by acting on the injection rate.
  • the reaction chamber opens into a smoke evacuation circuit which includes a gas outlet pipe opening into a device for recovering solid particles entrained with the gases.
  • This recovery device can for example be a cyclone which comprises an upper orifice for leaving gases and very fine particles and a lower orifice for leaving solid particles having a dimension greater than a certain limit which depends on the performance of the recovery device.
  • the solid particles thus recovered are returned to the fluidized bed, at the base of the reaction chamber, by a recycling circuit. In this way, the incompletely burned particles are recycled at the base of the reaction chamber, in the combustion zone, the fumes causing only the finest ashes.
  • the operating mode of the fluidized beds is linked to the injection rate and to the gas circulation speed. If the injection rate is adjusted so that the gas speed is only a little higher than the critical speed from which fluidization begins, most of the solid particles remain at the base of the reaction chamber under form a dense fluidized bed, only very fine particles being entrained with the gases.
  • the fluidization speed exceeds a limit which depends on the average size of the particles and which is of the order of 4 m / s, most of the particles are entrained with the fumes and then a distinction is made between inside the reaction chamber a dense lower zone surmounted by a dilute zone traversed by an ascending current of gases and particles which escapes through the outlet pipe, the solid particles being separated from the gases in the recovery device and returned to the dense area of the fluidized bed, at the base of the reaction chamber, by the recycling circuit. We then have a so-called running bed operation.
  • Circulating fluidized beds have a number of known advantages. In particular, they allow greater power than ordinary dense beds, the volume of the combustion chamber being better used since the reaction can occur not only in the dense bed, at the bottom of the reaction chamber, but also in the given area. ' The circulating beds are also more flexible because they make it possible to vary the speed of the gases, and to adjust the circulation rate and therefore the residence time of the fuel.
  • the efficiency of a combustible material treatment installation and in particular of a gasification installation depends on the average residence time of the particles which must be greater than the gasification time, the latter depending on the nature of the fuel and the average particle size.
  • DE-C-919 004 discloses a gasifier comprising a chamber in which a fluidized bed is provided above a fluidization grid.
  • This assembly comprises, below the grid, gasification means with endothermic reaction and, above the grid, gasification means with exothermic reaction.
  • the dust entrained by the gases is recovered in a cyclone and reintroduced into the fluidized bed.
  • a coolant is introduced to the upper part of the gasification chamber so as to avoid the deposit of sticky ash on the walls.
  • the high temperature zone is limited to the dense fluidized bed where one can reach a temperature from which the ash gradually agglomerates.
  • This has the advantage of allowing the disposal of the ashes having formed blocks of a certain size and which can be removed by a purge placed at the base of the reaction chamber.
  • the homogenisation of temperatures may not be effective enough to prevent localized overheating and therefore happens in some regions in a fusion of ash that can go all the blocking of the reactor.
  • the invention relates to a new method for operating in a circulating bed at the highest possible temperature so that the particles remain as long as possible at this high temperature without risk of sticking.
  • the temperature is relatively uniform over the entire circuit of materials
  • This cooling does not significantly decrease the yield of the reaction since the high temperature is maintained not only in the dense area of the fluidized bed but also in the diluted area.
  • the reaction can thus take place as long as possible at high temperature, the risk of sticking being less in the zones where the particles are in agitation and separated from each other.
  • reaction temperature it is therefore possible to adjust the reaction temperature to the highest possible level and in particular to a level allowing the agglomeration of the ash into blocks capable of being removed by known means, without however reaching the melting temperature which would risk cause a blockage of the reactor.
  • the bonding temperature depends on the operating conditions and therefore, having observed these, it will be possible to determine in each zone of the installation, according to the circumstances specific to this zone, the temperature limit at not to exceed.
  • the temperatures will preferably be controlled in at least one zone A at the base of the reaction chamber, that is to say in the dense zone of the fluidized bed, a zone B slightly above the level limit of the dense zone, a zone C in the diluted zone, at the upper part of the reaction chamber and a zone D just upstream of the recovery device.
  • a cold product in divided form will be injected into it, which may consist, for example, of water spray or steam, of particles recovered and cooled before being recycled in the fluidized bed or by a part of the gas produced, taken at the outlet of the recovery device and recycled in the desired zone after cooling.
  • the cold product injected can also consist of at least part of the combustible material introduced into the upper part of the diluted zone in the reaction chamber with an adjustable flow rate so that the coarsest particles fall into the dense zone. of the fluidized bed while crossing the diluted zone, the particles the finest being entrained with the fumes to the recovery device and then recycled into the fluidized bed.
  • the invention also covers an improved installation for processing combustible material, conventionally constituted by a vertical reaction chamber provided with means for supplying solid combustible material and, at its base, means for fluidization by injection of a gas with an adjustable flow rate and connected at its upper part, by a flue outlet pipe to a device for recovering entrained solid materials, comprising an upper outlet, a lower outlet for solid particles connected by a recycling circuit to the base of the reaction chamber.
  • the installation comprises, upstream of the recovery device, a plurality of zones (A, B, C, D, ...) of temperature control, staggered in the direction of circulation of the gases and materials and each covering the entire cross section of the gas passage at the level in question, each control zone (A, B, C, D, ...) being provided with a means of measuring the average ambient temperature and a means of cooling causing a localized lowering of this ambient temperature in the zone considered and that the temperature measurement and cooling means of the control zones are associated with a regulation device comprising a set of comparators of the temperatures measured with reference temperatures determined in depending on the desired operating conditions in each control zone (A, B, C, D, ...), a set of adjustment means for the cooling means and a means for controlling the adjustment means in function ction of the differences observed between the measured temperatures and the reference temperatures.
  • the single figure schematically represents a gasification plant for coal in a fluidized bed provided with improvements according to the invention.
  • the gasification installation essentially comprises a reaction chamber 1 in the form of a column, consisting of an elongated cylindrical enclosure with a vertical axis provided at its base with a grid for the homogeneous distribution of a fluidization gas introduced below the grate with a flow rate adjustable by injection means 11.
  • the reaction chamber 1 is connected at its upper part, by a flue outlet pipe 12, to a device 2 for recovering entrained solid particles, for example a dust collector cyclone comprising an upper outlet 21 for the gases and a lower outlet 22 for the recovered particles which opens into a recycling pipe 23 connected to the base of the chamber 1 by a device for reinjecting solid particles consisting for example of a siphon 24 in which can be injected into a gas allowing adjustment of the reinjection rate.
  • the combustible material, stored in a hopper 13 is introduced at the base of the combustion chamber, into the fluidized bed, for example by means of a screw feed device 14 making it possible to adjust the feed rate by acting on the speed of rotation of the screw.
  • a purge line 18 placed at the lower end of the combustion chamber 1 makes it possible to remove the agglomerated ash.
  • the flow rate of the fluidizing gas injection member 11 is adjusted so that the installation operates in a circulating bed, the gas circulation speed being greater than 4 m / s so that the gases entrain the most large part of the solid particles which then occupy the entire height of the column 1 inside which there is a lower zone 15 in the dense phase and an upper zone 16 in the diluted phase.
  • the combustible material introduced into the chamber 1 is divided into two parts: the finer particles are immediately entrained with the gases while the larger particles fall into the dense zone 15 and remain there until, after partial combustion, they reach a dimension which allows them to be trained in turn.
  • the dense zone can also contain an inert granular material serving as a support for fluidization or else having a role in the reaction.
  • the solid particles entrained in the outlet pipe 12 are stopped in the recuperator 2 and then recycled in the fluidized bed through the pipe 24.
  • control zones (A, B, C, D) are placed respectively, on the one hand at least at three levels of the reaction chamber 1, respectively in (A) in the dense part of the fluidized bed, in (B) at the boundary surface of it and in
  • the dense area of the fluidized bed contains the largest particles of fuel and inert material and is traversed by the recycled fine particles consisting of incompletely burnt material and ash. It is desirable to maintain in this zone a temperature for which the ashes are sufficiently softened to allow their agglomeration, however, avoiding their merger or solidification. In fact, by agglomerating, the ash forms blocks which are easier to remove, but too high a temperature rise could cause the ash to melt and stick together between them and on the walls of the reactor with the risk of blocking it.
  • the solid particles carried away by the gaseous fluid are found at substantially the same temperature as in the dense zone 15 and are therefore agglomerating: their concentration being lower and their agitation significant, the tendency to agglomeration is less but it is also necessary to avoid sticking of the particles on the walls of the reactor, in particular in the critical zones which it is possible to locate.
  • a number of temperature sensors 31, 32, 33, 34 can be placed in the most sensitive parts of the installation.
  • a sensor 31 was placed in the center of the dense area 15, a sensor 32 at the bottom of the diluted area 16, slightly above the limit level of the dense area, a sensor 33 at the upper end of the reaction chamber 1, near the outlet flue and a sensor 34 at the inlet of the recuperator 2 near the wall.
  • the set of sensors is connected to a measuring device 3 providing at its output signals corresponding to the temperatures measured by each of the sensors, which are applied to a set of members 41, 42, 43, 44 for comparing each signal of temperature with a displayed signal corresponding to the reference temperature determined for the zone considered.
  • This intervention means consists, in the example shown, of a cooling circuit 5 comprising a fan 51, the supply line 52 of which is connected to the sheath 26 of the gas outlet from the separator 2 in order to take off part of the evacuated gases, these having preferably been cooled by means of an exchanger 27 placed on the outlet sheath 26 upstream of the supply line 52.
  • the discharge line 5 of the fan 51 is divided into a number of branches 6 provided at their ends with injectors 61, 62, 63, 64 opening into the various zones of the installation, substantially at the height of the corresponding temperature sensor.
  • each injection branch 6 with a plurality of injectors distributed regularly in a plane transverse to the axis so that the injected cooling fluid is spread evenly throughout the cross section of the installation at the height of the area considered.
  • the members 61 62, 63, 64 make it possible to inject a product in divided form throughout the zone and at a temperature below the temperature measured in the control zone. Given the homogenizing effect of the temperatures obtained in addition by the use of a high fluidization speed, it will thus be possible to control the temperature fairly precisely inside each zone of the installation, on the entire cross section of the gas passage.
  • each branch 6 of the cooling circuit will be provided with a valve 71, 72, 73, 74 controlled by a computer 7 as a function of the temperature differences measured by the comparators 41, 42, 43, 44.
  • the computer 7 is programmed to take account of the interactions between the zones, any cooling in one zone having repercussions in the following zones.
  • the temperature control of the different zones is obtained by injecting a portion of the fumes sampled at the outlet of the separator, after cooling to a temperature below ambient temperature in the different zones of the installation.
  • a fluid cooling agent such as water vapor or water spray
  • the latter could for example be provided with an exchanger 28 making it possible to bring the temperature of the recycled particles at the desired level.
  • solid particles or water are preferably injected in the gas or liquid phase to control agglomeration.
  • water or recycled gas will be injected, via the injectors 63 or 64, to avoid sticking and accumulation in the separator.
  • the injections individually or in combination with one another, by acting either on the flow rate injected if the cooling agent is a gas or water spray, or, preferably, on the temperature if the coolant consists of recycled solid particles.
  • part of the fuel taken from the feed circuit thereof and injected at 17, preferably at the top of the diluted zone 16, can also be used as a cooling product.
  • the installation according to the invention has only been described schematically, the devices used such as the regulation system and the means for cooling and injecting the recycled product being able to be produced with known means.
  • the invention could be the subject of variants and improvements, and, for example, the reaction chamber could be divided into a greater number of temperature control zones staggered from bottom to top to 1 inside the dense zone and especially in the diluted zone of the fluidized bed.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Gasification And Melting Of Waste (AREA)

Claims (13)

1. Verfahren zur Verarbeitung eines brennbaren Stoffes im Wirkbelbett in einer Anlage, die eine vertikale Reaktionskammer (1), die an ihrem unteren Teil mit Einrichtungen (14) zur Versorgung mit dem brennbaren Stoff und Einrichtungen (11) zur Wirbelbildung über das Einblasen eines Gases versehen und am oberen Ende über eine Gasauslaßleitung (12) mit einer Vorrichtung (2) zum Rückgewinnen der mitgeführten Feststoffteilchen verbunden ist, die eine Gasauslaßmündung (21) und eine Auslaßmündung (22) für die Feststoffteilchen umfaßt, die über einen Rückführungskreislauf (23) mit dem unteren Teil der Reaktionskammer (1) verbunden ist, dadurch gekennzeichnet, daß unter Berücksichtigung der Art des brennbaren Stoffes und der Arbeitsverhältnisse wie beispielsweise der Form und der Abmessungen der Anlage, der Korngröße der Teilchen und der Geschwindigkeit der Gaszirkulation eine Bezugstemperatur bestimmt wird, ab der die unbeweglichen Stoffteilchen einem Zusammenbacken im unteren Teil der Rückgewinnungsvorrichtung (2) ausgesetzt sind, die Wirbelbildungsverhältnisse reguliert werden, um eine Arbeit der Anlage in Form eines Zirkulationsbettes zu verwirklichen, die Temperatur der Reaktion im dichten Teil (15) des Wirbelbettes auf eine Höhe über der Bezugstemperatur eingestellt wird, die mittleren Temperaturen in einer Vielzahl von Zonen (A, B, C, D) zur Temperaturüberwachung stufenförmig in Richtung der Zirkulation des Gases und der Stoffe im Inneren der Anlage gemessen werden, jede gemessene Temperatur mit der bestimmten Bezugstemperatur verglichen wird, und örtlich in der einen oder anderen Zone stromaufwärts von der Rückgewinnungsvorrichtung (2) die mittlere Temperatur jedesmal dann herabgesetzt wird, wenn die gemessene Temperatur dort die Bezugstemperatur erreicht, um permanent die mittlere Temperatur in dieser Zone unter der entsprechenden Bezugstemperatur zu halten.
2. Verarbeitungsverfahren nach Anspruch 1, dadurch gekennzeichnet, daß man die Reaktionstemperatur im dichten Teil (15) des Wirbelbettes auf einen Wert regelt, der eine Klumpenbildung der Ascheteilchen in Blöcken erlaubt, die abgeführt werden können.
3. Verarbeitungsverfahren nach Anspruch (1), dadurch gekennzeichnet, daß die Messung der mittleren Temperaturen in den Zonen (A, B, C, D...) derart erfolgt, daß die Temperaturen wenigstens in einer Zone (A) am unteren Teil der Reaktionskammer (1) in der dichten Zone der Wirbelbettes, in einer Zone (B) etwas über der Grenzhöhe dieser dichten Zone, in einer Zone (C) im oberen Teil der Kammer (1) und in einer Zone (D) direkt stromaufwärts von der Rückgewinnungsvorrichtung (2) überwacht werden.
4. Verarbeitungsverfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß die örtliche Herabsetzung der Temperatur dadurch erfolgt, daß in die betrachtete Zone ein Kühlmittel in verteilter Form eingegeben wird.
5. Verarbeitungsverfahren nach Anspruch 4, dadurch gekennzeichnet, daß das eingegebene Kühlmittel aus einem Wassersprühnebel oder Wasserdampf besteht.
6. Verarbeitungsverfahren nach Anspruch 4, dadurch gekennzeichnet, daß das eingegebene Kühlmittel aus den Teilchen besteht, die am Ausgang der Rückgewinnungsvorrichtung (2) rückgewonnen und nach einer Abkühlung in die Wirbelbett zurückgeführt werden.
7. Verarbeitungsverfahren nach Anspruch 4, dadurch gekennzeichnet, daß das eingegebene Kühlmittel aus einem Teil des Gasproduktes besteht, der am Ausgang der Rückgewinnungsvorrichtung (2) abgezogen und in die gewünschte Zone nach einer Abkühlung rückgeführt wird.
8. Verarbeitungsverfahren nach Anspruch 4, dadurch gekennzeichnet, daß das eingegebene Kühlmittel aus wenigstens einem Teil des brennbaren Stoffes besteht, der am oberen Teil der verdünnten Zone (16) der Reaktionskammer (1) in einer einstellbaren Menge eingeführt wird, wobei die größeren Teilchen in die dichte Zone (15) des Fluidbettes nach unten fallen, wobei sie die verdünnte Zone (16) durchqueren, und die feineren Teilchen mit den Abgasen zur Rückgewinnungsvorrichtung (2) mitgerissen werden, um in das Wirbelbett (15) rückgeführt zu werden.
9. Anlage zum Verarbeiten eines brennbaren Stoffes mit einer vertikalen Reaktionskammer (1), die mit Versorgungseinrichtungen (14) für einen festen, brennbaren Stoff und am unteren Teil mit Einrichtungen (11) zur Wirbelbildung durch Einblasen eines Gases in einstellbarer Menge versehen und am oberen Teil über eine Auslaßleitung (12) für die Abgase mit einer Vorrichtung (2) zum Rückgewinnen der mitgeführten Feststoffe verbunden ist, die einen oberen Ausgang (21) und einen unteren Ausgang (22) für die Feststoffteilchen aufweist, der über einen Rückführungekreislauf (23) mit dem unteren Teil der Reaktionskammer (1) verbunden ist, dadurch gekennzeichnet, daß sie stromaufwärts der Rückgewinnungsvorrichtung (2) ein Vielzahl von Zonen (A, B, C, D...) zur Temperaturüberwachung stufenweise in Richtung der Zirkulation des Gases und des Stoffes umfaßt, die den ganzen Querschnitt der Gasdurchgangs auf der betreffenden Höhe überdecken, wobei jede Überwachungezone (A, B, C, D...) mit einer Einrichtung (31, 32, 33, 34) zum Messen der mittleren Umgebungstemperatur und mit einer Abkühlungseinrichtung (61, 62, 63, 64) versehen ist, die eine örtliche Abnahme dieser Umgebungstemperatur in der betreffenden Zone hervorruft, und daß die Temperaturmeßeinrichtungen (31, 32, 33, 34) und die Abkühlungseinrichtungen (61, 62, 63, 64) der Überwachungszonen mit einer Regeleinrichtung verbunden sind, die eine Gruppe von Kompevatoren (41) zum Vergleichen der gemessenen Temperaturen mit Bezugstemperaturen, die als Funktion der gewünschten Arbeitsverhältnisse in jeder Überwachungszone (A, B, C, D...) bestimmt sind, eine Gruppe von Regelgliedern für die Abkühlungseinrichtungen (61, 62, 63, 64) und eine Einrichtung (7) zum Steuern der Regelglieder in Abhängigkeit von den Unterschieden umfaßt, die zwischen den gemessenen Temperaturen und den Bezugstemperaturen festgestellt werden.
10. Anlage nach Anspruch 9, dadurch gekennzeichnet, daß die Überwachungszonen (A, B, C, D...) jeweils einerseits auf wenigstens drei Höhen der Verbrennungskammer, jeweils bei (A) im dichten Teil des Fluidbettes, bei (B) an deren Grenzfläche und bei (C) am Ausgang der Verbrennungskammer und andererseite bei (D) in der Rückgewinnungsvorrichtung (2) angeordnet sind.
11. Verarbeitungsanlage nach Anspruch 9, dadurch gekennzeichnet, daß die Einrichtung zur örtlichen Abkühlung für jede Überwachungszone (A, B, C, D...) aus einem Element (61, 62, 63, 64) besteht, das in die gesamte Zone ein Produkt in verteilter Form einführt, das eine Temperatur hat, die unter der in der Überwachungszone gemessenen Temperatur liegt.
12. Verarbeitungsanlage nach Anspruch 9 und 10, dadurch gekennzeichnet, daß die Abkühlungseinrichtungen ein Organ (27) zum Abkühlen der den Abscheider verlassenden Abgase und einen Kreislaut (5) umfassen, der einen Teil der Abgase nach einer Abkühlung abzieht und mehrere Zweigleitungen (6) umfaßt, die jeweils in der betreffenden Zone der Anlage über zwischengeschaltete Einblasdüsen (61, 62, 63,64) münden und jeweils mit einem Steuerglied (71, 72, 73, 74) für die Einblasmenge versehen sind, das über eine Regeleinrichtung (7) in Abhängigkeit von den in der betreffenden Zone gemessenen Temperaturen angesteuert wird.
13. Verarbeitungsanlage nach einem der Ansprüche 9 bis 12, dadurch gekennzeichnet, daß jede Überwachungszone (A, B, C, D..,) den gesamten Querschnitt des Gasdurchgangs an der betreffenden Stelle der Anlage überdeckt.
EP84400961A 1983-05-17 1984-05-11 Verfahren und Vorrichtung zur Behandlung eines Brennstoffes in einer Wirbelschicht Expired EP0126001B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84400961T ATE32606T1 (de) 1983-05-17 1984-05-11 Verfahren und vorrichtung zur behandlung eines brennstoffes in einer wirbelschicht.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8308166 1983-05-17
FR8308166A FR2546177B1 (fr) 1983-05-17 1983-05-17 Procede et installation perfectionnee de traitement d'une matiere combustible en lit fluidise

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EP0126001A1 EP0126001A1 (de) 1984-11-21
EP0126001B1 true EP0126001B1 (de) 1988-02-24

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EP (1) EP0126001B1 (de)
AT (1) ATE32606T1 (de)
BR (1) BR8402303A (de)
CA (1) CA1270699A (de)
DE (1) DE3469442D1 (de)
FR (1) FR2546177B1 (de)
IN (1) IN161204B (de)
ZA (1) ZA843725B (de)

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FI86105C (fi) * 1985-11-19 1992-07-10 Ahlstroem Oy Foerfarande och anordning foer reglering av en virvelbaeddsreaktors funktion.
EP0311599B1 (de) * 1985-12-09 1990-11-07 A. Ahlstrom Corporation Reaktor mit zirkulierendem wirbelbett, verfahren zum trennen von feststoffen aus rauchgas
US4763585A (en) * 1987-09-08 1988-08-16 Ogden Environmental Services Method for the combustion of spent potlinings from the manufacture of aluminum

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Publication number Priority date Publication date Assignee Title
DE1074803B (de) * 1960-02-04 Badische Anilin- &. Soda-Fabrik Aktiengesellschaft, Ludwigshafen/Rhein Verfahren zur Brenngaserzeugung durch Vergasen feinzerteilter fester oder flüssiger Brennstoffe und/oder durch Spalten gasförmiger Brennstoffe in einer Wirbelschicht
DE919004C (de) * 1951-11-10 1954-10-11 Basf Ag Verfahren und Vorrichtung zum Vergasen koerniger Brennstoffe
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
GB2027444B (en) * 1978-07-28 1983-03-02 Exxon Research Engineering Co Gasification of ash-containing solid fuels
DE2925441C2 (de) * 1979-06-23 1982-10-14 Carbon Gas Technologie GmbH, 4030 Ratingen Verfahren und Vorrichtung zum Vergasen von Kohle in einer Wirbelschicht
JPS5776088A (en) * 1980-10-31 1982-05-12 Nippon Kokan Kk <Nkk> Coal gasification using powdered coal and its device

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ZA843725B (en) 1984-12-24
IN161204B (de) 1987-10-17
BR8402303A (pt) 1984-12-26
DE3469442D1 (en) 1988-03-31
FR2546177A1 (fr) 1984-11-23
CA1270699A (fr) 1990-06-26
ATE32606T1 (de) 1988-03-15
FR2546177B1 (fr) 1987-07-17
EP0126001A1 (de) 1984-11-21

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