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EP0214417A2 - Procédé de production de gaz de synthèse à partir de combustibles solides - Google Patents

Procédé de production de gaz de synthèse à partir de combustibles solides Download PDF

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Publication number
EP0214417A2
EP0214417A2 EP86109953A EP86109953A EP0214417A2 EP 0214417 A2 EP0214417 A2 EP 0214417A2 EP 86109953 A EP86109953 A EP 86109953A EP 86109953 A EP86109953 A EP 86109953A EP 0214417 A2 EP0214417 A2 EP 0214417A2
Authority
EP
European Patent Office
Prior art keywords
fixed bed
gasification
bed
solid
fluidized bed
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.)
Ceased
Application number
EP86109953A
Other languages
German (de)
English (en)
Other versions
EP0214417A3 (fr
Inventor
Johannes Dr. Rer. Nat. Dipl.-Phys. Teggers
Johannes Dr.-Ing. Dipl.-Ing. Lambertz
Lothar Dr. Rer. Nat. Dipl.-Chem. Schrader
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.)
Rheinbraun AG
Original Assignee
Rheinische Braunkohlenwerke 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 Rheinische Braunkohlenwerke AG filed Critical Rheinische Braunkohlenwerke AG
Publication of EP0214417A2 publication Critical patent/EP0214417A2/fr
Publication of EP0214417A3 publication Critical patent/EP0214417A3/fr
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • 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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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

Definitions

  • the invention relates to a process for the production of synthesis gas from solid fuels at elevated pressure in a fluidized bed using endothermic and exothermic reacting gasification agents, a post-gasification chamber being provided above the fluidized bed and a fixed bed made of the solid gasification residues below the fluidized bed and the fuels in the gas Fluidized bed introduced, the solid gasification residues are withdrawn from the fixed bed and the synthesis gas generated is withdrawn from the post-gasification room.
  • the solid gasification residues forming the fixed bed located below the fluidized bed consist predominantly of mineral accompanying substances of the fuels, i.e. their ashes and mineral admixtures, although there is also a certain proportion of C-containing solids in the fixed bed. There may be coarser grits that fall down through the fluidized bed onto the fixed bed due to their greater weight. Another part of the C-containing particles in the fixed bed will consist of smaller grains, the C content of which has been largely, but not completely, converted in the gasification process.
  • Such interruptions in operation may take days, given the need to allow the reactor to cool after the gasification process is interrupted, etc.
  • the procedure is generally such that exothermic gasifying agent, that is oxygen, is blown in above the upper limit of the fixed bed in such a way that a reaction of this oxygen with C-containing particles still present in the fixed bed is avoided in any case. This means that oxygen is only introduced into the fluidized bed and possibly into the post-reaction space above it.
  • the level of the upper limit of the fixed bed is to be kept more or less constant during the duration of the gasification process, it is necessary that as much material is withdrawn from the fixed bed below and thus removed from the gasification process as material from above from the fluidized bed the fixed bed. Compliance with this condition has not presented any particular difficulties in the gasification reactors previously operated in practice because the solid fuel introduced into the gasification process was more or less uniform in nature over long periods of time. This means that the relationship between the carbon and the unreachable mineral substances, in particular ash and possibly other mineral substances, remained more or less constant over long periods. In many cases this has been achieved by taking appropriate precautions during the extraction of the solid fuels, for example coal or peat, in the deposit. In other cases, the coal coming from the deposit has been subjected to a processing process which has ensured the consistent quality of the solid fuel, also in the sense of the aforementioned relationship between C and non-gasifiable mineral substances.
  • the absolute and relative proportion of unreachable mineral accompanying materials in the fuel is not a problem, so that fuels with a poorer quality compared to the previously used fuels in terms of higher ash content for the extraction of Synthesis gas could be used.
  • This is very desirable even for reasons of cost, since fuels with a higher ballast component are noticeably cheaper.
  • this increases the cost of the fuel used in the gasification process, which at least largely eliminates the cost advantage of low-quality coal, which must also be used for the gasification process for reasons of economy.
  • the proportion of non-gasifiable minerals that fluctuates over the duration of the gasification process has the disadvantage in the process management hitherto customary that the height of the fixed bed and thus the level of the upper limit thereof is subject to unpredictable and uncontrollable fluctuations which depend on the fluctuations in the content of non-gasifiable constituents of the fuel introduced into the carburetor. This means that compliance with the condition required for a trouble-free operation of the gasification process to keep the upper limit of the fixed bed below a level at which it comes into contact with oxygen-containing gasification agent is no longer guaranteed.
  • the height of the fixed bed rises to such an extent that at least its upper area reaches a zone into which oxygen-containing gasifying agent is blown, since the lower section normally flows in this zone the fluidized bed.
  • This increase in the fixed bed is due to the fact that the non-gasifiable mineral substances, insofar as they are accompanying minerals, i.e. have not grown into the coal, immediately fall through the fluidized bed down to the fixed bed as soon as they enter the reactor, since they are noticeably higher have a specific weight than those particles which consist entirely or predominantly of carbon.
  • the higher proportion of non-gasifiable substances can also have the effect that the carbon-containing particles have a higher ash content, so that this also increases the proportion of solid gasification residues that get into the fixed bed and thus leads to an increase in the fixed bed and thus to a shift of the upper limit of the same leads upwards.
  • This accumulation of carbon-containing particles in the upper region of the fixed bed is due in particular to the fact that a gas is normally passed through the fixed bed from bottom to top, which is intended to prevent the solid bed from solidifying too strongly, but without loosening it up to the extent that it physically Has the properties of a fluidized bed.
  • a gas is normally passed through the fixed bed from bottom to top, which is intended to prevent the solid bed from solidifying too strongly, but without loosening it up to the extent that it physically Has the properties of a fluidized bed.
  • this gas passed through the fixed bed which may also have the function of a cooling medium, it is in many cases an endothermic gasifying agent, for example CO2 or steam.
  • the invention is based on a method of the type described in the introduction. It is based on the object of improving this method in such a way that solid fuels can also be used which have a strongly fluctuating content of non-gasifiable solids, without the trouble-free course of the Gasification process experiences a noticeable impairment.
  • the invention proposes that the speed at which the fixed gasification residues forming the fixed bed are withdrawn from the gasification process is regulated in dependence on the height of the fixed bed in such a way that the upper limit of the fixed bed remains below that range which oxygen-containing gasification agent is introduced into the gasification process.
  • the rate at which the solid gasification residues are withdrawn from the gasification process or the reactor depends on the proportion of the amount of the unreactable constituents of the carbon-containing material introduced into the gasification process.
  • the height of the fixed bed is recorded and used as a control variable.
  • a procedure has been found to be particularly expedient in which the temperature in the fixed bed area is used as the measured value for determining the position of the upper limit of the fixed bed.
  • Such a procedure is based on the fact that the temperature in the fluidized bed is normally higher than that in the fixed bed, due to the exothermic reactions taking place in the fluidized bed.
  • the fixed bed is noticeably cooler. This applies in particular if use is made of the possibility already mentioned of allowing a gasifying agent which brings about endothermic reactions to flow through the fixed bed, since the reactions of this gasifying agent with the carbon-containing particles still present in the fixed bed lead to a noticeable reduction in temperature.
  • the temperature difference between the fluidized bed and the upper section of the fixed bed will be in the order of 100-300 ° C.
  • Another possibility is to use the pressure drop along the fixed bed as a measured value for determining the position of the upper limit of the fixed bed. This makes use of the fact that this pressure drop in the fixed bed is noticeably lower than in a corresponding distance of the same height in the fluidized bed.
  • the gasification process for the production of synthesis gas takes place in a reactor 10, in whose lower region 12, which tapers conically from top to bottom, is the fluidized bed (fluidized bed) 14.
  • the conical region 12 is adjoined at the top by a cylindrical region 16 which contains the post-gasification zone 18.
  • the reactor 10 merges into a downpipe 20, the two sections of which open into a conveyor and cooling screw 22. Through the downpipe 20 and the screw 22, the solid gasification residues are drawn off, which collect below the fluidized bed 14 in a fixed bed 24.
  • the solid fuel to be gasified is introduced into the reactor 10 from a reservoir 28 by a screw 26.
  • the solid fuel enters the latter at a noticeable distance below the upper limit 30 of the fluidized bed 14.
  • the reactor 10 is provided with several feed lines for gaseous media.
  • the leads 32 located at the bottom open into the two sections of the downpipe 20. They are used to supply a gaseous medium to loosen the fixed bed 24.
  • This medium can be an endothermic gasifying agent, for example steam or CO2, but also an inert one Medium, e.g. B. nitrogen act. The latter can e.g. B. come into question if the product gas produced in the reactor 10 is used for the ammonia synthesis.
  • Additional feed lines 44, 45, 46, 47 are assigned to the after-reaction space 18. They normally introduce gasifying agents which bring about exothermic and endothermic reactions into the after-reaction zone 18.
  • the solid fuel introduced into the reactor 10 by the screw 26 first reaches the fluidized bed 14, in which the fuel particles are generated by the gasification agents, the degassing products, by vaporization of the water contained in the fuel, and the reaction products is fluidized.
  • the very small, ie dust-like components of the fuels introduced into the fluidized bed are entrained relatively quickly by the gas flowing upwards through the upper boundary of the fluidized bed 30 into the after-reaction space 18, in which they are largely converted.
  • the extent to which gasifying agent is fed into the post-reaction space 18 depends in particular on the amount of carbon to be converted in the post-reaction space 18.
  • the heavier particles fall down through the fluidized bed 14 onto the fixed bed 24.
  • These heavier particles can be coarser, predominantly carbon-containing particles that are too large to be separated from the gas flowing from the bottom of the fluid bed upwards could be worn.
  • such particles sediment downward through the fluidized bed 14 onto the fixed bed 24, the weight of which is too high in relation to the grain size.
  • these can be carbon-containing particles with a high ash content. But it can also be such particles such.
  • B. act grains of sand that consist exclusively of non-gasifiable substances.
  • the product gas generated in the reactor 10 is withdrawn through a line 50 located near the upper end of the reactor 10 and after pre-cleaning in a cyclone 52 downstream devices, for. B. for gas cleaning.
  • the solid particles deposited in the cyclone 52 which generally still contain C, can be returned via a line 54 into the fluidized bed 14 and thus into the reactor 10.
  • temperature sensors 57, 58, 59 are mounted in planes which have relatively small vertical distances from one another.
  • the upper limit of the fixed bed 24 would lie approximately in the area of the plane 60, naturally due to the fact that all solid parts in the reactor 10 are in constant motion upper limit of the fixed bed will never run exactly on one level.
  • the nozzles located at the bottom, through which gasification agent which brings about endothermic reactions is fed in via the feed line 34. It applies to all blowing planes or areas that the nozzles are advantageously distributed over the circumference of the reactor.
  • a section 62 is provided in the lower part of the conical region 12, which is delimited on the underside by the plane 60 and on the top side by a second plane 61 which is at a distance therefrom.
  • This section 62 defines the area within which the height of the fixed bed 24 varies depending on the proportion of the non-gasifiable materials contained in the supplied fuel. That is, depending on the proportion of non-gasifiable materials, section 62 either from fluidized bed 14 or is filled by the fixed bed 24 or in its upper area by the fluidized bed 14 and in its lower area by the fixed bed 24.
  • the lower temperature sensor 59 is arranged approximately at the level of the lower limit of the region 62.
  • the upper temperature sensor 57 is located approximately at the level 61 which defines the upper limit of the fluctuation range 62.
  • a third temperature sensor 58 is arranged approximately in the middle of the vertical fluctuation range 62.
  • the temperature sensors 57, 58 and 59 are connected via lines 64 and a controller 66 which influences the drive 68 of the conveyor and cooling screw 22.
  • the temperature sensor 59 will display a lower temperature than the temperature sensors 57 and 58 arranged above it, which are then in the region of the fluidized bed 14, which is down to approximately under the aforementioned condition extends to level 60.
  • the fact that in the lower region of the fluidized bed 14 through the feeds 34, 36, and 38 are fed exclusively gasifying agents which bring about endothermic reactions is irrelevant, since a uniform temperature is largely present within the fluidized bed.
  • the fluidized bed 14 is characterized by a high thermal conductivity.
  • the height of the fixed bed 24 also increases, assuming that the screw conveyor 22 is running at a constant speed. That is, its upper boundary moves toward the level 61. As soon as the upper limit of the fixed bed 24 reaches the area of the temperature sensor 58, this indicates a decrease in the temperature, which is used via the controller 66 to influence the drive 68 of the screw conveyor 22 in the sense of an increase in the delivery capacity. This means that more solid gasification residues are discharged from the fixed bed 24 per unit of time.
  • the upper limit of the fixed bed 24 will remain approximately at the level of the temperature sensor 58 until the amount of non-gasifiable materials supplied changes again. If the increased conveying speed of the screw conveyor 22 leads to the fact that more solid gasification residues are withdrawn from the fixed bed than per unit time of non-gasifiable materials with the fuel are introduced into the reactor, the upper limit of the fixed bed 24 decreases until the lower limit of the fluidized bed 14 den Temperature sensor 59 reached. The temperature increase thereby caused in the area of the temperature sensor 59 is then used again by the controller 66 to reduce the conveying speed of the screw conveyor 22 accordingly.

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  • 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)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP86109953A 1985-09-02 1986-07-19 Procédé de production de gaz de synthèse à partir de combustibles solides Ceased EP0214417A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3531292 1985-09-02
DE19853531292 DE3531292A1 (de) 1985-09-02 1985-09-02 Verfahren zur herstellung von synthesegas aus festen brennstoffen

Publications (2)

Publication Number Publication Date
EP0214417A2 true EP0214417A2 (fr) 1987-03-18
EP0214417A3 EP0214417A3 (fr) 1987-07-01

Family

ID=6279937

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86109953A Ceased EP0214417A3 (fr) 1985-09-02 1986-07-19 Procédé de production de gaz de synthèse à partir de combustibles solides

Country Status (8)

Country Link
EP (1) EP0214417A3 (fr)
CN (1) CN86105030A (fr)
AU (1) AU6212586A (fr)
BR (1) BR8604177A (fr)
DD (1) DD259205A1 (fr)
DE (1) DE3531292A1 (fr)
FI (1) FI863502L (fr)
ZA (1) ZA866607B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
WO2008095977A1 (fr) * 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Procédé et dispositif de gazéification à flux entraîné de combustibles solides sous pression
WO2019097326A1 (fr) * 2017-11-17 2019-05-23 Universidad Pedagogica Y Tecnologica De Colombia Uptc Gazéification de matière carbonée mélange de biomasse et de charbon minéral au moyen d'un four à flux forcé de type cyclone

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4013224A1 (de) * 1990-04-26 1991-10-31 Abb Patent Gmbh Messung der wirbelschichthoehe in einem pyrolysereaktor
DE4340459C1 (de) * 1993-11-27 1995-05-18 Rheinische Braunkohlenw Ag Verfahren zum Betreiben eines Wirbelschichtreaktors zum Vergasen von kohlenstoffhaltigen Einsatzstoffen
DE4413923C2 (de) * 1994-04-21 2001-11-29 Rheinische Braunkohlenw Ag Verfahren zum Erzeugen von Synthese- und/oder Brenngas in einem Hochtemperatur-Winkler-Vergaser
DE19548324C2 (de) * 1994-12-23 1998-08-06 Rheinische Braunkohlenw Ag Verfahren zum Vergasen von kohlenstoffhaltigen Feststoffen in der Wirbelschicht sowie dafür verwendbarer Vergaser
CN101701161B (zh) * 2009-10-20 2013-07-17 江汉大学 采用黄姜废渣或中药材废渣生产可燃气的装置与方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3855070A (en) * 1971-07-30 1974-12-17 A Squires Hydropyrolysis of hydrocarbonaceous fuel at short reaction times
DE2741805A1 (de) * 1977-09-16 1979-03-29 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum vergasen von festem, kohlenstoffhaltigem material
EP0041094A1 (fr) * 1980-06-03 1981-12-09 Westinghouse Electric Corporation Enlèvement des particules à partir de systèmes à couche fluidisée
EP0093801A2 (fr) * 1982-05-11 1983-11-16 KRW Energy Systems Inc. Régulation de la hauteur d'un lit fluidisé d'un système de gazéification

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2856059A1 (de) * 1978-12-23 1980-07-10 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum kuehlen fester vergasungsrueckstaende
US4433978A (en) * 1982-01-21 1984-02-28 Westinghouse Electric Corp. Fluidized bed gasification ash reduction and removal system
DE3241239A1 (de) * 1982-11-09 1984-05-10 Carbon Gas Technologie GmbH, 4030 Ratingen Vorrichtung zum austragen von feststoffen aus einem wirbelschichtreaktor

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3855070A (en) * 1971-07-30 1974-12-17 A Squires Hydropyrolysis of hydrocarbonaceous fuel at short reaction times
DE2741805A1 (de) * 1977-09-16 1979-03-29 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum vergasen von festem, kohlenstoffhaltigem material
EP0041094A1 (fr) * 1980-06-03 1981-12-09 Westinghouse Electric Corporation Enlèvement des particules à partir de systèmes à couche fluidisée
EP0093801A2 (fr) * 1982-05-11 1983-11-16 KRW Energy Systems Inc. Régulation de la hauteur d'un lit fluidisé d'un système de gazéification

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
WO2008095977A1 (fr) * 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Procédé et dispositif de gazéification à flux entraîné de combustibles solides sous pression
US20100088959A1 (en) * 2007-02-07 2010-04-15 Technische Universitat Bergakademie Freiberg Method and Device for the Entrained-Flow Gasification of Solid Fuels under Pressure
AU2008212869B2 (en) * 2007-02-07 2012-05-24 Technische Universitat Bergakademie Freiberg Method and device for the entrained-flow gasification of solid fuels under pressure
EA017334B1 (ru) * 2007-02-07 2012-11-30 Технише Университет Бергакадеми Фрайберг Способ и установка для газификации твёрдого топлива в потоке под давлением
CN101605876B (zh) * 2007-02-07 2013-07-10 北卡德米弗莱贝格工业大学 在加压下对固体燃料进行气流床气化的方法和装置
US8518134B2 (en) 2007-02-07 2013-08-27 Technische Universität Bergakademie Freiberg Method and device for the entrained-flow gasification of solid fuels under pressure
WO2019097326A1 (fr) * 2017-11-17 2019-05-23 Universidad Pedagogica Y Tecnologica De Colombia Uptc Gazéification de matière carbonée mélange de biomasse et de charbon minéral au moyen d'un four à flux forcé de type cyclone

Also Published As

Publication number Publication date
ZA866607B (en) 1987-04-29
FI863502A0 (fi) 1986-08-29
FI863502L (fi) 1987-03-03
DD259205A1 (de) 1988-08-17
EP0214417A3 (fr) 1987-07-01
AU6212586A (en) 1987-03-05
BR8604177A (pt) 1987-04-28
DE3531292C2 (fr) 1990-08-09
DE3531292A1 (de) 1987-03-12
CN86105030A (zh) 1987-03-04

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