EP2281864B1 - Procédé et dispositif de gazage de combustibles solides - Google Patents

Procédé et dispositif de gazage de combustibles solides Download PDF

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Publication number
EP2281864B1
EP2281864B1 EP09167484.6A EP09167484A EP2281864B1 EP 2281864 B1 EP2281864 B1 EP 2281864B1 EP 09167484 A EP09167484 A EP 09167484A EP 2281864 B1 EP2281864 B1 EP 2281864B1
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EP
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Prior art keywords
gas
reactor
fixed
gasification
reactor chamber
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EP09167484.6A
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German (de)
English (en)
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EP2281864A1 (fr
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Walter Sailer
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Individual
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Individual
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Priority to EP09167484.6A priority Critical patent/EP2281864B1/fr
Application filed by Individual filed Critical Individual
Priority to HUE09167484A priority patent/HUE034286T2/en
Priority to PL09167484T priority patent/PL2281864T3/pl
Priority to LTEP09167484.6T priority patent/LT2281864T/lt
Priority to DE202009012833U priority patent/DE202009012833U1/de
Priority to SI200931655T priority patent/SI2281864T1/sl
Priority to DK09167484.6T priority patent/DK2281864T3/en
Publication of EP2281864A1 publication Critical patent/EP2281864A1/fr
Application granted granted Critical
Publication of EP2281864B1 publication Critical patent/EP2281864B1/fr
Priority to HRP20170732TT priority patent/HRP20170732T1/hr
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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
    • C10J3/02—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • 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
    • C10J3/725—Redox processes
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/0916—Biomass
    • 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

Definitions

  • the present invention relates to a device according to the preamble of claim 1 and a method according to the preamble of claim 8.
  • the invention thus relates to a method and to the devices of a working in vacuum autothermal DC fixed-bed gasifier with internal circulation to produce a nearly tar-free wood gas from wood chips or woody biomass for motor use, which produces mainly by optimizing the thermochemical process of gas reduction becomes.
  • the goal is to increase the continuous production of wood gas with high quality and quantity by the gas reduction, which can be finally used with little effort of a dry gas treatment (dedusting and cooling) in internal combustion engines to generate electricity and heat.
  • An alternative is also the utilization of the wood gas for biodiesel production, e.g. according to Fischer Tropsch method.
  • a method of the type described above is known in which a gasification agent is injected into the middle region of a fixed bed reactor and is divided into a first and a second partial flow.
  • the first partial stream withdrawn above is postoxidized in an oxidation chamber and subsequently added to the second partial stream.
  • the resulting gas mixture is aftertreated in a fluidized bed reactor.
  • the method described in this document is complex in terms of apparatus and requires in addition to the fixed bed reactor, a separate oxidation chamber and a fluidized bed reactor. It is an object of the invention to provide a process for the gasification of solid fuels, which has a high efficiency and results in a high quality end product.
  • a three-stage pyrolysis reactor is known in which pyrolysis gas is sucked up, in the upper third air is blown, in the lower third air is blown with the externally guided down pyrolysis and down clean gas is withdrawn.
  • the construction of this device is relatively complex, since several blowers are provided to move the individual gas streams.
  • a complex temperature management is required by the outward gas streams. Due to the three-stage nature of the process, the reactor as a whole builds relatively high.
  • the device of a spacious pan grate allows sufficient formation of a continuous charcoal emberstock as a reduction zone to produce a nearly tar-free wood gas by a full gas reduction requiring only a dry gas treatment.
  • This method with the internal gas circulation constructive devices and the intensive diffuser injector injection of the raw gases into the oxidation zone utilizing the injector flow energy for conveying, mixing and blowing as well as the continuous charcoal stock formation in the large scale Sink grate as a reduction zone largely meets the requirements of ideal conditions of the catalytic and thermal gas formation processes to produce a nearly tar-free product gas.
  • These temperature zones which are passed through the carburettor fuel wood chips are generally the drying zone at temperatures up to 200 ° C, the pyrolysis (decomposition, degassing) at temperatures between 200 ° C - 700 ° C, the oxidation zone or combustion zone at temperatures up to 1300 ° C. and the reduction zone at temperatures between 500 ° C - 600 ° C.
  • the combustible gas mixture produced from the reduction zone is discharged or sucked off substantially vertically in direct current through the grate or its slots for gas treatment.
  • the coal dust with the resulting wood ash is separated from the gas mixture.
  • the multi-stage gasification plant DE 102 58 640 A1 the split into two partial gas streams in a countercurrent process and down from the fixed bed in a DC process.
  • the volume ratios are used throttle bodies.
  • the upwardly led partial gas stream is fed via the fuel bed for separate oxidation in an oxidation chamber and substoichiometrically oxidized by addition of combustion air at 1100 ° C - 1,300 ° C, so as to crack or oxidize the unwanted, long-chain hydrocarbon compounds can.
  • a second untreated partial gas stream is converged downwardly from the fixed bed gasifier in direct co-current with the first hot exhaust gas from the oxidation chamber and mixed.
  • the downwardly diverted partial gas stream also serves as a transport medium for the required Reduktionskoks in the reduction chamber, which is mixed with the first treated water vapor-rich gas stream is introduced for common gas reduction in the downstream reduction chamber.
  • the pneumatic transport of the coke is supported by the supply of the exhaust gas from the oxidation chamber, wherein the formed as a fluidized bed reduction reactor with the incoming and koksstructureden gas forms the combustible gas components H2 and CO.
  • This multi-stage gasification process by separation of the gas streams into individual reaction chambers by means of the control by throttle bodies is very expensive for the cracking or oxidation of undesirable long-chain hydrocarbon compounds with subsequent gas reduction and is known to be applied to fluidized bed gasifiers.
  • the tarry-rich carbonization and pyrolysis gases are mixed with the gasification medium (blowing medium) by suction through the eight arranged diffuser nozzles and blown the carburetor in the oxidation zone for combustion or energy production with pressure energy. Due to the intensive turbulence of the gas mixture, as in the case of an oil burner, complete combustion of the tar-containing raw gases or cracking of the long-chain hydrocarbon chains occurs in the oxidation zone.
  • the diffuser injection nozzles simultaneously effect by suction, mixing and blowing of the media a constant internal circulation of the gas streams in the reactor and thus a uniform temperature distribution, a complete flow of the thermochemical reactions with a sufficient Verändauer to reduce gas.
  • the device of a spacious 8eckigen tub grid for receiving a sufficient charcoal embers stock as a reduction zone for gas production.
  • this device of a spacious 8-sided bath grid provides the prerequisite for complete gas reduction and thus the production of a virtually tarry product gas.
  • the transition from the oxidation zone into the reduction zone in the area of the bottle-neck constriction with the conclusion of the oblique trapezoidal 8eckigen grid grid also allows a homogeneous temperature distribution and intensive flow of gases, whereby the interactions of the reactions between oxidation and reduction are optimized for gas reduction.
  • Compared to the multi-stage gasification plant DE 102 58 640 A1 differs the DC fixed-bed gasifier with internal circulation of the swelling and pyrolysis gas to the effect that no external separation of the gas streams for a separate gas treatment (oxidation-reduction chamber) is present, no throttle bodies and no pneumatic transport of coke for a formed as a fluidized bed reduction reactor, but the Optimization of all interactions between oxidation and reduction or the complex gas formation processes to obtain a nearly tar-free wood gas take place in a gasification reactor.
  • the wood gas producer corresponds EP 0 693 545 A1 in which, in the area of the constriction in the gasifier chamber, a gas ring channel is provided for combustion of tar constituents, not the present invention, when a gas mixture is blown into the oxidation zone for complete combustion by means of an 8-jet nozzle ring with diffuser injection nozzles.
  • the process and the technical devices can be used to produce the required operating conditions for the interaction between oxidation and reduction or the catalytic and thermal gasification processes such as the Boudouard equilibrium, the water gas equilibrium and the methane equilibrium under favorable conditions for investment and operation unburned hydrocarbons or tar distillates in the wood gas are given more.
  • the pressureless-autothermal DC fixed-bed gasifier reactor space 2 has with the refractory lining 9 a bottle neck shape - comparable to the blast furnace. This constriction in the transition zone of the oxidation zone in the reduction zone is an intense mass transfer between the reacting surface of the charcoal stock and the gas components (CO2, H2O) to form the gas reduction (CO, H2, CH4).
  • Fig. 1 is fed via a conveyor belt continuously carburetor fuel, consisting of lumpy wood chippings of the largely airtight fire-proof double-slider lock 10, which is introduced after reporting the paddle 8 in the reactor chamber 2.
  • the gasification material in the reactor chamber 2 passes from top to bottom through the zones of drying, pyrolysis (decomposition, degassing), oxidation and reduction.
  • pyrolysis decomposition, degassing
  • oxidation and reduction oxidation and reduction.
  • temperatures up to more than 1200 ° C. form on the nozzle level in the ember bed above the sump grate 3, with the energy released keeping the gasification processes of the individual zones going.
  • the resulting swelling and pyrolysis gases rise countercurrently in the upper gasification chamber 7.
  • a spacious grid in the form of a 8eckigen tub 3 is placed with oblique side walls in which continuously forms a charcoal stock as a reduction zone or as a catalyst for gas reduction.
  • the product gas formed in the reduction zone exits downwards in the prevailing negative pressure operation, which is generated by the suction motor or exhaust gas fan.
  • the product gas leaves the gas outlet via the refractory opening 14, the lateral gas outlet pipe 25 and is supplied to a gas cleaning or cooling before use in the motor thermal power plant.
  • the wood ash produced during combustion and during gas production as well as the dusty and coarse-grained charcoal are carried along as abrasion.
  • the coarse-grained charcoal ash with ash falls into the inclined part of the ash shaft 13 below the reactor.
  • the ash and the coarse-grained Holzkohleabrieb is promoted and disposed of via a motor 19 operated with screw 18 in the gas-tight ash container 20.
  • the side channels 6 are protected by covers 16, as well as the gas outlet opening 14 of the gas outlet nozzle 25 is protected from the ingress of ash and carbon fiber by a cover 15.
  • the bottleneck-shaped constriction over the pan grate also causes an intensive material flow changes, the homogeneous temperature distribution the pyrolysis gas and gasification gas mixture and the glowing charcoal as a reduction zone allows further cleavage of residual tars.
  • the internal circulation of the gas streams for splitting the hydrocarbons or tars additionally improves this process.
  • an optimal temperature distribution in the reactor with a uniform complete sequence of the reactions and a sufficient residence time of the gases in the reaction zones is possible.
  • An essential aspect is that the apparatus of the reactor vessel 1 from a cylindrical steel jacket, a bottle neck refractory wall 9 of the carburetor chamber 2 with vertical side channels 6, a ring pipe 4 to the carburetor, designed as 8-jet nozzle ring with uniformly distributed diffuser injector 5 (injector) for sucking out the swelling pyrolysis gases 7 (conveying medium) by the gasification agent 4 (blowing medium) and producing a gas mixture 22 of both media and blowing the gas mixture (diffuser-printing energy effect) into the oxidation zone, a double-slide lock 10 for introducing the carburetor fuel into the gasifier space 2, which is burned or gassed in the drying, pyrolysis and oxidation zones and continuously formed by the stoichiometric combustion of the carburetor fuel in the 8-cornered trapezoidal furnace grid 3 is a charcoal lump as a reduction zone for gas production around the process, in which by the
  • the device of a nozzle ring 4, 5 (FIG. Fig. 2 ) is arranged evenly distributed around the gasification reactor with at least eight injector injection nozzles 5, which is connected to a ring pipe 4 lying outside the reactor and a centrally connected preheated gasification leads, in which the gas mixture 22 with the Schwell- and pyrolysis gases in the middle of Oxidation zone is injected into the carburetor and a controllable safety technology is ensured by this design.
  • the device of a spacious 8eckigen oblique trapezoidal Feuerungsrostes with slot openings in the form of a trough 3 is centrally located in the middle of the gasification reactor, a movable base of the Feuerungsrostes by hand or motor 12 to eliminate interference from slag and Aschenansammlungen in which in comparison to the oxidation and pyrolysis zone, a proportionally oversized amount of a glowing charcoal cane is upstream as a reduction zone, which renews continuously by substoichiometric combustion of the carburetor fuel and thus as a catalyst a largely perfect reduction of the oxidation products (CO2, H2O) to produce a almost tarry product gas (CO, H2, CH4).
  • CO2, H2O oxidation products
  • CO, H2, CH4 almost tarry product gas
  • the device of an ash shaft 13 in the lower part of the carburetor below the tub grid 3 fulfills the task of receiving the ash or carbon abrasion caused by the combustion of the carburetor fuel in the Wannerost 3 or by the abrasion caused by the suction of the Product gas in the vacuum mode by the slot-shaped Wannerost 3 falls on the underlying ash shaft 13 and is disposed of continuously via an ash screw 18 with motor drive 19 in the gas-tight ash container 20.
  • the device is a largely airtight fire-proof double-slider lock 10 with motor drive, the feed of the gasification reactor with carburetor fuel, which is on the removable Cover 23, 24 of the steel cylinder is placed and the lower slide lock against radiation of hot gases with a fire-resistant, movable plate 11 is shielded.
  • the device for gasification reactor Fig. 1 from serviceischen reasons in three constructive components can be dismantled, namely an upper part with the cover 24 and double slide lock 10, a middle part of a sheet steel cylinder ring 1 with a refractory lining 9 in bottle neck shape 17 and integrated vertical side channels 6 and a lower part in which the diffuser Injector-Einblasdüsen 5 with the ring pipe network 4, 8eckigen Wannerost 3, the connected ash shaft 13 with gas outlet nozzle 14, 25 and ash removal 18, 19, 20 and all components form a unit.
  • the device of the inner lining 9 of the reactor space is designed in the shape of a bottle neck, are integrated in the vertical side channels for the internal circulation of gases in the vacuum operation, rests on the 8eckigen Sink grid 3 and thereby an intensive material flow change for a homogeneous temperature distribution, which prevents bridging and the burning out of cavities.
  • the invention relates to an autothermic vacuum-operated fixed-bed DC gasifier with internal gas circulation for producing a virtually tar-free wood gas from biomass with the devices according to FIG Fig. 1 , a reactor chamber 2 with bottle neck lining 9 and integrated vertical side channels 6, a double slide lock 10 for introducing the carburetor fuel and an injector consisting of a at least 8-jet diffuser-injector nozzle ring 4, 5 for sucking and mixing the swelling and pyrolysis gases 7 with the gasification agent 5, the gas mixture 22 injected with pressure into the oxidation zone, the nozzle ring with a pipe ring outside the carburetor connected to preheated carburetor supplied, a proportionally oversized 8eckigen Wannenrostes 3 for receiving the charcoal embers as a reduction zone for sufficient gas reduction.
  • the process of internally circulating the swelling and pyrolysis gases 7 with the gasification agent 4 through the injector conveyor sucks, mixes and injects the gas mixture into the oxidation zone for co-combustion with the gasoline fuel, thereby cracking the tars or hydrocarbons. a uniform temperature distribution, sufficient residence time is given for a complete reduction of gas in the reduction zone in the spacious pan grate.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (10)

  1. Dispositif servant à la gazéification de combustibles solides, en particulier de biomasse, se présentant sous la forme d'un gazéificateur à lit fixe à courant continu autothermique fonctionnant en pression négative, avec un réacteur à lit fixe, qui présente une chambre de réacteur (2) avec une section supérieure (2a) faisant office de zone d'oxydation et une section inférieure (2b) faisant office de zone de réduction, dans lequel des buses d'injection de diffuseur-injecteur (5) sont prévues pour injecter un agent de gazéification (4), lesquelles sont disposées dans une zone centrale de la chambre de réacteur (2) entre la section supérieure (2a) et la section inférieure (2b), et dans lequel au moins une ouverture de sortie supérieure est prévue dans la section supérieure, laquelle est en communication avec au moins une ouverture de retour (22) dans la zone centrale de la chambre de réacteur (2), dans lequel les buses d'injection de diffuseur-injecteur (5) servant à injecter l'agent de gazéification débouchent dans l'au moins une ouverture de retour (22), et au moins une ouverture de sortie inférieure est prévue dans la section inférieure, caractérisé en ce que l'au moins une ouverture de sortie supérieure est en communication avec l'au moins une ouverture de retour (22) dans la zone centrale de la chambre de réacteur (2) par l'intermédiaire de canaux latéraux verticaux internes dans le réacteur à lit fixe, et en ce que l'ouverture de sortie supérieure est en communication exclusivement avec l'au moins une ouverture de retour (22).
  2. Dispositif selon la revendication 1, caractérisé en ce que les buses d'injection de diffuseur-injecteur (5) sont disposées de manière uniformément répartie autour de la périphérie de la chambre de réacteur sous la forme d'une couronne de buses.
  3. Dispositif selon l'une quelconque des revendications 1 ou 2, caractérisé en ce que la section inférieure de la chambre de réacteur est réalisée sous la forme d'une grille de cuve (3) de préférence octogonale.
  4. Dispositif selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'ouverture de sortie supérieure est en communication avec l'au moins une ouverture de retour (22) par l'intermédiaire de canaux latéraux (6), qui sont disposés à l'intérieur d'une enveloppe en tôle d'acier de forme cylindrique et à l'extérieur d'une chemise (9) réfractaire.
  5. Dispositif selon l'une quelconque des revendications 1 à 4, caractérisé en ce qu'en dessous de la grille de cuve (3) est disposé un puits à cendres (13) servant à recevoir des résidus solides, lequel est en communication avec un bac à cendres (20) étanche aux gaz par l'intermédiaire d'une vis de décendrage (18).
  6. Dispositif selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'alimentation en combustible de la chambre de réacteur (2) se fait par l'intermédiaire d'un double sas (10).
  7. Dispositif selon l'une quelconque des revendications 1 à 6, caractérisé en ce qu'une chemise (9) de la chambre de réacteur (2) est réalisée sous la forme d'un goulet de bouteille.
  8. Procédé servant à la gazéification de combustibles solides, en particulier de biomasse, dans un gazéificateur à lit fixe à courant continu autothermique fonctionnant en pression négative selon l'une quelconque des revendications 1 à 7, où un gaz de gazéification, de préférence de l'air, est injecté dans une section centrale d'une chambre de réacteur (2) d'un réacteur à lit fixe et où un premier flux partiel du gaz injecté est guidé vers le haut à contre-courant et est évacué du réacteur à lit fixe sous la forme d'un gaz de pyrolyse (7) et où un deuxième flux partiel du gaz injecté est guidé vers le bas dans le sens direct et est évacué du réacteur à lit fixe, caractérisé en ce que le premier flux partiel (7) est guidé vers le bas à l'extérieur de la chambre de réacteur (2) par l'intermédiaire de canaux latéraux verticaux internes dans le réacteur à lit fixe et est réintroduit conjointement avec l'agent de gazéification (4) dans la chambre de réacteur (2), dans lequel le premier flux partiel est renvoyé par l'effet d'injection de l'agent de gazéification (4) dans le réacteur à lit fixe et dans lequel les buses d'injection de diffuseur provoquent une circulation interne permanente des flux de gaz par aspiration, mélange et injection des milieux dans le réacteur.
  9. Procédé selon la revendication 8, caractérisé en ce que le gaz de pyrolyse (7) du premier flux partiel est renvoyé en totalité dans le réacteur à lit fixe.
  10. Procédé selon l'une quelconque des revendications 8 ou 9, caractérisé en ce que l'agent de gazéification (4) est préchauffé avant l'injection dans le réacteur à lit fixe.
EP09167484.6A 2009-08-07 2009-08-07 Procédé et dispositif de gazage de combustibles solides Active EP2281864B1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
HUE09167484A HUE034286T2 (en) 2009-08-07 2009-08-07 Method and apparatus for gasification of solid fuels
PL09167484T PL2281864T3 (pl) 2009-08-07 2009-08-07 Sposób i urządzenie do zgazowywania paliw stałych
LTEP09167484.6T LT2281864T (lt) 2009-08-07 2009-08-07 Kietojo kuro dujinimo būdas ir įrenginys
DE202009012833U DE202009012833U1 (de) 2009-08-07 2009-08-07 Vorrichtung zur Vergasung fester Brennstoffe
EP09167484.6A EP2281864B1 (fr) 2009-08-07 2009-08-07 Procédé et dispositif de gazage de combustibles solides
DK09167484.6T DK2281864T3 (en) 2009-08-07 2009-08-07 Solid fuel gasification process and apparatus
SI200931655T SI2281864T1 (sl) 2009-08-07 2009-08-07 Postopek in naprava za uplinjanje trdih kuriv
HRP20170732TT HRP20170732T1 (hr) 2009-08-07 2017-05-16 Metoda i uređaj za prevođenje čvrstih goriva u plinovito stanje

Applications Claiming Priority (1)

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EP09167484.6A EP2281864B1 (fr) 2009-08-07 2009-08-07 Procédé et dispositif de gazage de combustibles solides

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EP2281864A1 EP2281864A1 (fr) 2011-02-09
EP2281864B1 true EP2281864B1 (fr) 2017-03-01

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DE (1) DE202009012833U1 (fr)
DK (1) DK2281864T3 (fr)
HR (1) HRP20170732T1 (fr)
HU (1) HUE034286T2 (fr)
LT (1) LT2281864T (fr)
PL (1) PL2281864T3 (fr)
SI (1) SI2281864T1 (fr)

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Publication number Priority date Publication date Assignee Title
US9115321B2 (en) 2010-02-16 2015-08-25 Big Dutchman International Gmbh Gasification device and method
DE202011004328U1 (de) * 2011-03-22 2012-06-25 Big Dutchman International Gmbh Schachtvergaser zum Betrieb bei einer unterstöchiometrischen Oxidation
CN102530863B (zh) * 2011-12-17 2013-08-14 湖北宜化化工股份有限公司 间歇式固定床分段、分区域制取合成氨原料气装置及方法
DE102011121992B4 (de) * 2011-12-22 2015-02-19 Josef Wagner Thermochemische Holzvergasungsanlage mit Festbettreaktor mit doppelt aufsteigender Gegenstromvergasung, Gasreinigung, Gasbereitstellung, Schadstoffverwertung und Schadstoffentsorgung für den Dauerbetrieb mit Gas-Kolbenmotoren und Gasturbinen
CN103666570B (zh) * 2012-09-20 2016-07-20 广州薪光合环保技术有限公司 自烘干式生物质气化系统
CN103666569B (zh) * 2012-09-20 2016-09-07 广州薪光合环保技术有限公司 生物质气化系统
KR102233960B1 (ko) * 2020-11-25 2021-03-30 (주)이씨티 바이오매스 가스화 시스템의 애쉬 제거 장치
AT526206A1 (de) * 2022-06-08 2023-12-15 Gs Gruber Schmidt Gmbh Vorrichtung einer Vergasungsanlage die auch als Pyrolyseanlage betrieben werden kann

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DE636763C (de) * 1932-10-04 1936-10-15 Bohumil Fleiser Gaserzeuger fuer bituminoese Brennstoffe mit abwaerts gerichtetem Zuge

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DE9411856U1 (de) 1994-07-22 1994-09-22 Viesel, Manfred, 72574 Bad Urach Holzgaserzeuger
DE19718184C2 (de) * 1997-04-30 2003-05-28 Inst En Und Umwelttechnik E V Vorrichtung zur energetischen Nutzung von Brennstoffen, insbesondere Biobrennstoffen
DE10258640A1 (de) 2002-12-13 2004-06-24 Björn Dipl.-Ing. Kuntze Verfahren und Vorrichtung zur Erzeugung von Brenngas aus festen Brennstoffen
GR1005536B (el) * 2006-03-07 2007-06-07 Λαμπρος Ελευσινιωτης Διβαθμιος συνδυασμενος αεριοποιητης ομορροης -αντιρροης
EP2126008A2 (fr) 2007-03-06 2009-12-02 Lampros Elefsiniotis Gazogène à trois phases et lit fixe, qui comprend une zone tampon du courant gazeux entre la zone de pyrolyse et la zone de combustion

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DE636763C (de) * 1932-10-04 1936-10-15 Bohumil Fleiser Gaserzeuger fuer bituminoese Brennstoffe mit abwaerts gerichtetem Zuge

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SI2281864T1 (sl) 2017-08-31
LT2281864T (lt) 2017-07-25
DE202009012833U1 (de) 2010-01-21
PL2281864T3 (pl) 2017-09-29
DK2281864T3 (en) 2017-06-19
EP2281864A1 (fr) 2011-02-09
HRP20170732T1 (hr) 2017-07-28
HUE034286T2 (en) 2018-02-28

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