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EP3548587B1 - Procédé et appareil de réduction de carbone dans le produit inférieur d'un gazéificateur à lit fluidisé - Google Patents

Procédé et appareil de réduction de carbone dans le produit inférieur d'un gazéificateur à lit fluidisé Download PDF

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Publication number
EP3548587B1
EP3548587B1 EP17811206.6A EP17811206A EP3548587B1 EP 3548587 B1 EP3548587 B1 EP 3548587B1 EP 17811206 A EP17811206 A EP 17811206A EP 3548587 B1 EP3548587 B1 EP 3548587B1
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EP
European Patent Office
Prior art keywords
combustion chamber
fluidized
gasification reactor
bed combustion
additional
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.)
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Application number
EP17811206.6A
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German (de)
English (en)
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EP3548587A1 (fr
Inventor
Ralf Abraham
Domenico Pavone
Dobrin Toporov
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.)
Gidara Energy BV
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Gidara Energy BV
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Priority to PL17811206T priority Critical patent/PL3548587T3/pl
Publication of EP3548587A1 publication Critical patent/EP3548587A1/fr
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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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10J3/52—Ash-removing devices
    • C10J3/523—Ash-removing devices for 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
    • 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
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • 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
    • C10J3/50—Fuel charging devices

Definitions

  • the present disclosure relates to a plant for converting carbonaceous fuels into synthesis gas comprising a gasification reactor with at least one fluidized bed zone in which the fuels are gasified by suitable gasification means, a carbonaceous ash stream being produced as the bottom product in a bottom area below the fluidized bed zone and with below the gasification reactor a device is arranged in which the bottom product is oxidized by supplying an oxidizing agent.
  • Winkler process is considered a tried and tested technology with which both lumpy and liquid or pasty fuels are converted into synthesis gas.
  • Difficult fuels with a very high ash content and biologically based fuels are also used as fuel. These are introduced into a fluidized bed, which is operated as a bubble-forming fluidized bed, and gasified with oxygen.
  • the HTW process works at comparatively moderate temperatures, at which the resulting ash does not leave the gasification reactor in a molten state. This has operational advantages, particularly with corrosive ash.
  • the gasification usually takes place via separate nozzles with the gasification agents, for example water vapor, carbon dioxide, oxygen or air.
  • the gasification agents for example water vapor, carbon dioxide, oxygen or air.
  • These nozzles are arranged, for example, in different levels, for example both in the fluidized bed zone and in the so-called freeboard zone (FB).
  • FB freeboard zone
  • FB freeboard zone
  • a high material and energy transfer rate is achieved and by returning the unconverted solids via the cyclone and return line to the fluidized bed, a uniform temperature distribution across the fluidized bed can be ensured.
  • the temperature of the fluidized bed should be kept below the temperature of the ash softening point.
  • gasification agents usually oxygen
  • oxygen are introduced into the FB zone, which is located above the fluidized bed.
  • various effects are achieved, namely, on the one hand, the conversion of part of the finely divided fuel that is discharged from the fluidized bed and, on the other hand, the temperature of the gases should be increased so that further oxidation and / or the volatile substances (tars and hydrocarbons) expelled from the feedstock can crack.
  • the finely distributed fuel particles react with steam and CO 2 in accordance with the Boudouard reaction.
  • the proportion of total oxygen above the fluidized bed is, for example, between about 60% and about 10% in an HTW process.
  • the temperatures should preferably not exceed certain limit values, and the operating temperature should preferably be at least about 100 ° C. below the ash softening point. This can be done by mixing steam with oxygen and introducing it into the reactor.
  • the addition of oxygen to the post-gasification zone also leads in side reactions to a partial combustion of the synthesis gas reservoir (CO + H 2 ) and consequently to a reduction in the synthesis gas yield. Therefore, one has to increase the gas and particle temperature in order to accelerate the gasification reaction.
  • WO 2015/003778 A1 describes a method and a device for the aftertreatment of the carbon-containing soil product resulting from the gasification of carbon-containing fossil fuels in a high-temperature Winkler process (HTW process) in the direction of gravity below the fluidized bed. It is proposed to use the energy of the soil product and to achieve the landfill suitability not to feed the soil product to an external furnace, but to apply an oxidizing agent to open-pore ceramic elements such as gas purging stones, foam ceramics or the like in a soil product oxidizer below the fluidized bed. In this way, a more extensive oxidation is to be achieved and the carbon conversion in the HTW gasifier is to be increased.
  • HTW process high-temperature Winkler process
  • U.S. 4,721,514 A describes a method for gasifying coal using coal powder.
  • the object of the present invention is to provide an improved device and a method for the economical gasification of different starting materials in a pressurized fluidized bed gasification, which is suitable for comparatively high operating pressures of preferably above 10 bar and is economical with a high level of safety and availability.
  • an additional fluidized bed combustion chamber is arranged as a device for oxidizing the bottom product below the fluidized bed zone of the gasification reactor.
  • an effective combustion of the bottom product from the gasification reactor can be achieved by supplying a suitable oxidizing agent.
  • the reactor forming the additional fluidized bed combustion chamber is preferably somewhat smaller than the gasification reactor.
  • This additional fluidized bed combustion chamber is positioned below the gasification reactor and is connected to the fluidized bed zone of the gasification reactor, for example via a cross-sectional constriction.
  • the oxidizing agent which is fed into the additional fluidized bed combustion chamber via the at least one feed device, preferably sprayed or injected, preferably comprises oxygen and / or air and can additionally contain, for example, steam and / or CO 2 . If several feed devices are used, oxidizing fluid streams with different compositions can be fed from one or several of the aforementioned gases / fluids are fed to the additional fluidized bed combustion chamber.
  • the oxygen content of the oxidizing agent when this is fed in as a mixture with steam, is preferably less than about 21% by volume.
  • the oxygen content and the amount of oxygen should be selected depending on the amount of carbon in the bottom product to be burned in the additional fluidized bed combustion chamber and the combustion temperature below the ash softening.
  • a preferred development of the invention provides that the system has at least one temperature measuring device for measuring the temperature in the additional fluidized bed combustion chamber.
  • This temperature measuring device can be used to measure the temperature in the additional fluidized bed combustion chamber and, depending on the temperature measured, the carbon content of the fuel can be deduced and the oxygen content of the oxidizing agent supplied can be adjusted accordingly, preferably so that hyperstoichiometric ratios result.
  • a regulating device is preferably also provided to regulate the amount and / or the oxygen content of an oxygen and / or air and / or steam and / or CO 2 -containing fluid flow injected into the additional fluidized bed combustion chamber via the at least one feed device .
  • the control device is preferably in operative connection with the temperature measuring device in order to measure the amount and / or the oxygen content of the oxygen and / or air and / or steam and / or CO 2 injected into the additional fluidized bed combustion chamber via the at least one feed device To regulate fluid flow as a function of the measured temperature in the additional combustion chamber.
  • the feed device is designed such that the bottom product to be burned in the additional combustion chamber is fluidized by the oxygen and / or air and / or steam and / or CO 2 -containing fluid flow injected into the additional fluidized bed combustion chamber.
  • the feed device preferably comprises at least one nozzle, preferably a multi-component nozzle, for injecting a fluid mixture of at least two different oxidizing fluids into the additional combustion chamber.
  • a multi-fluid nozzle can be used here, as shown in the WO 2014/026748 A1 is described. Reference is expressly made here to the content of this publication.
  • At least one valve for shutting off and / or regulating the oxidizing fluid flow fed in is preferably assigned to the feed device, so that the feed of the oxidizing agent can be regulated and / or shut off if necessary.
  • the system according to the invention comprises at least two supply devices for supplying differently composed oxidizing fluid flows, each supply device being assigned at least one valve for shutting off and / or regulating the respectively supplied oxidizing fluid flow.
  • each supply device being assigned at least one valve for shutting off and / or regulating the respectively supplied oxidizing fluid flow.
  • the system according to the invention preferably comprises at least one pressure difference measuring device and display device in order to display a pressure difference between the pressure in the fluidized bed of the gasification reactor and the pressure in the additional fluidized bed combustion chamber.
  • the measured pressure difference can be used, for example, to optimize the conditions for the fluidization of the fluidized bed in the gasification reactor due to the flue gases emerging from the additional fluidized bed combustion chamber on the one hand and the oxidizing agent supplied on the other.
  • a preferred further development of the system according to the invention provides that it has at least one connecting line for the return of raw gas from the gasification reactor, the one from the gasification reactor and into the additional one Introduces fluidized bed combustion chamber.
  • at least a partial flow of the raw gases generated in the gasification reactor can be returned to the additional fluidized bed combustion chamber and used there, for example, for fluidization (generation of the fluidized bed) and / or possibly also for oxidation and promotion of combustion, provided the raw gas is still Contains oxidizing gas components.
  • a preferred further development of the system according to the invention comprises at least one compressor for compressing the raw gas that is returned from the gasification reactor into the additional fluidized bed combustion chamber, so that the raw gas can be compressed for the return.
  • the subject of the present disclosure is also a method for converting carbonaceous fuels into synthesis gas in which the fuels are gasified by suitable gasifying agents in a gasification reactor with at least one fluidized bed zone, with a floor area located below the fluidized bed zone a carbonaceous ash stream is obtained as the bottom product and a device is arranged below the gasification reactor in which an oxidation of the bottom product takes place by supplying an oxidizing agent, the oxidation of the bottom product taking place in an additional fluidized bed combustion chamber arranged below the fluidized bed zone of the gasification reactor.
  • the flue gas resulting from the oxidation of the bottom product in the additional fluidized bed combustion chamber is fed from the underside into the gasification reactor and serves to generate fluidization of the particles to be gasified or at least to support this fluidization.
  • part of the raw gas generated during gasification in the gasification reactor is returned from the gasification reactor via at least one connecting line to the additional fluidized bed combustion chamber.
  • the recirculated part of the raw gas generated during the gasification in the gasification reactor is preferably compressed by means of at least one compressor before it is introduced into the additional fluidized bed combustion chamber.
  • a preferred development of the method provides that the exit velocity of the bottom product from the gasification reactor into the additional fluidized bed combustion chamber located below is preferably adjusted with the aid of the flow of the recirculated gas in such a way that only particles of coarser particle size due to gravity from the gasification reactor into the one below get additional fluidized bed combustion chamber. The finer class of particles therefore remains in the gasification reactor, which also reduces the carbon content.
  • the method according to the invention provides that the fuel is preferably gasified in the gasification reactor at an operating pressure of at least approximately 10 bar.
  • an oxidizing fluid flow containing oxygen and / or air and / or steam is injected into the additional fluidized bed combustion chamber via at least one first supply device, and a fluid flow containing CO 2 and / or contains recycled gas from the gasification reactor.
  • the oxygen content of the oxidizing agent fed to the fluidized bed combustion chamber can be set in accordance with the carbon content of the fuel, with conditions preferably being set above stoichiometric.
  • the gasification reactor used for gasification in the fluidized bed zone according to the present invention is particularly preferably a high-temperature Winkler gasifier and the gasification process is carried out under appropriate conditions with regard to pressure, temperature and other parameters, reference being made here to the publication mentioned above and the relevant literature becomes.
  • FIG Figure 1 shows a schematically simplified illustration of an exemplary system according to the invention, the a conveyor system 20 by means of which the starting material, for example coal, biomass, waste or the like, is fed to the gasification reactor 10.
  • This conveying and supply system 20 comprises, for example, a number of conically ending containers 21 and optionally locks and is suitable for bringing the starting material to a pressure level that also prevails in the gasification reactor 10.
  • the material can then be brought into the gasification reactor via a screw conveyor 22.
  • the gasification reactor 10 comprises a fluidized bed zone 11 and above a so-called "free board zone", ie a mixing area 16 (also called freeboard zone), in these two zones 11, 16 the gasification of the starting material at elevated temperatures of, for example, about 800 ° C to about 1200 ° C takes place with the supply of a mixture of oxygen and steam or air. Furthermore, a cyclone separator 18 connected to the gasification reactor 10 is provided, in which the entrained partially gasified particles (ash particles) are separated from the synthesis gas generated in the gasification reactor so that the dust-free synthesis gas can be discharged via an outlet line 19. A return line 23 is provided, which starts from the lower region of the cyclone separator 18 and serves to return ash particles entrained with the synthesis gas, which were separated in the cyclone separator 18, into the fluidized bed zone 11.
  • a cyclone separator 18 connected to the gasification reactor 10 is provided, in which the entrained partially gasified particles (ash particles) are separated from the synthesis gas generated in the gas
  • solid by-products (ash particles) from the bottom product of the gasification reactor 10 reach an additional fluidized bed combustion chamber 12, which is arranged below the fluidized bed zone 11 of the gasification reactor 10 and is connected to it via a cross-sectional constriction, so that particles of the bottom product, in particular due to gravity can fall from the gasification reactor 10 downwards into the additional fluidized bed combustion chamber 12, while lighter, smaller particles remain in the gasification reactor 10 due to the fluidization.
  • the additional fluidized bed combustion chamber 12 is much smaller than the gasification reactor 10 and is only a fraction of the size of the gasification reactor.
  • the addition of the oxidizing agent which consists in particular of oxygen / steam, air or CO 2
  • the oxidizing agent can take place in different areas of the system at different height positions.
  • a first upper nozzle 24 for adding the oxidizing agent to the gasification reactor is provided in the lower region of the "free board zone".
  • a mixture of oxygen and steam for example, is added below it into the fluidized bed zone 11 of the gasification reactor via a second central nozzle 25 and a third central nozzle 26.
  • this or another oxidizing agent of one of the compositions described above is added via a fourth lower nozzle 27 is provided, which takes place directly into the additional fluidized bed combustion chamber 12.
  • These various nozzles for the supply of the oxidizing agent can in the simplest case be connected to one another via lines when using oxidizing agents of the same composition and fed via common supply lines, but a supply from different sources via separate line systems is equally possible.
  • a first upper feed device 24 can be seen in the form of a nozzle or the like for, for example, a mixture of oxygen and steam, which is injected into the fluidized bed zone 11 of the gasification reactor.
  • a further central feed device 26 is arranged, via which, in this case, a mixture of recycled raw gas and CO 2 from the Gasification reactor is fed, which is used here to support the fluidization of the material to be gasified in the fluidized bed zone 11.
  • a further lower nozzle 27 is provided, which is arranged on the outside of the additional fluidized bed combustion chamber 12 and via which oxidizing agent such as a mixture of oxygen and steam can be fed into the additional fluidized bed combustion chamber 12.
  • Another lower nozzle 28 is arranged in the lower region of the additional fluidized bed combustion chamber 12, via which, for example, a mixture of recycled raw gas from the gasification reactor and CO 2 can be injected into the additional fluidized bed combustion chamber.
  • a mixture of recycled raw gas from the gasification reactor and CO 2 can be injected into the additional fluidized bed combustion chamber.
  • the combustion residues / ash particles can be fluidized in the additional fluidized bed combustion chamber 12 and thus a fluidized bed can be formed.
  • a line 29, in which a valve 30 is arranged, leads to this nozzle 28, so that the supply to the nozzle 28 can be regulated and, for example, shut off or throttled.
  • This line 29 is connected to a line from which a branch line 31 branches off, which leads to the nozzle 26, so that a gas mixture from the gasification reactor can be used for fluidization in both parts of the plant, which is fed from the latter via a common line, which then branches off and leads to the nozzles 26 and 28, respectively.
  • a valve 32 is also arranged in the branch line 31, so that this branch line 27 can be shut off separately if, for example, only a supply to the nozzle 28 is desired. It is also possible via a further valve 35 to shut off the line before the branch line 31 branches off or to regulate the supply of raw gas and CO 2 for both lines 29, 31 already there.
  • a temperature measuring device 33 is provided, by means of which the temperature in the additional fluidized bed combustion chamber 12 can be measured.
  • the measured temperature can be used to draw conclusions about the carbon content of the fuel in the combustion chamber 12, from which it is then in turn calculated how much oxidizing agent must be supplied to the combustion chamber 12 via the nozzle 27 in order to achieve an optimal oxygen / carbon ratio (preferably if this is set above stoichiometric)
  • a pressure difference measuring device 34 which measures the respective pressure on the one hand in the fluidized bed zone 11 and on the other hand in the additional fluidized bed combustion chamber 12, the pressure difference between the two values being determined and displayed. From this pressure difference, conclusions can be drawn about the flow conditions in the cross-sectional constriction 13 between the two parts of the system. Depending on this, the supply of the fluid via the line 27 and the nozzle 26 into the area of the cross-sectional constriction 13 can then be regulated, which is done, for example, via the valve 32. In this way, one can influence the degree of fluidization of the fluidized bed zone 11 by the recycled raw gas.

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

Claims (15)

  1. Installation de conversion de combustibles carbonés en gaz de synthèse, comprenant un réacteur de gazéification (10) avec au moins une zone de lit fluidisé (11), dans laquelle les combustibles sont gazéifiés au moyen d'un agent de gazéification approprié, un flux de cendres carbonées étant obtenu comme produit de fond dans une région de fond disposée sous la zone de lit fluidisé (11) et un dispositif, dans lequel le produit de fond est oxydé au moyen d'une alimentation en agent oxydant, étant disposé sous le réacteur de gazéification (10), caractérisée en ce que
    - une chambre de combustion à lit fluidisé supplémentaire (12) est disposée comme un dispositif pour l'oxydation du produit de fond sous la zone de lit fluidisé (11) du réacteur de gazéification (10),
    - au moins un dispositif d'alimentation (27, 28) est prévu pour l'alimentation en oxygène et/ou en air et/ou en vapeur et/ou en CO2 dans la chambre de combustion à lit fluidisé supplémentaire (12), et
    - le dispositif d'alimentation (27, 28) est conçu de telle sorte que le produit de fond à brûler dans la chambre de combustion à lit fluidisé supplémentaire (12) est fluidisé grâce au flux de fluide contenant de l'oxygène et/ou de l'air et/ou de la vapeur et/ou du CO2 injecté dans la chambre de combustion à lit fluidisé supplémentaire (12).
  2. Installation de conversion de combustibles carbonés en gaz de synthèse selon la revendication 1, caractérisée en ce que la chambre de combustion à lit fluidisé supplémentaire (12) est reliée à la zone de lit fluidisé (11) du réacteur de gazéification (10) par un rétrécissement de section transversale (13).
  3. Installation de conversion de combustibles carbonés en gaz de synthèse selon la revendication 1 ou 2, caractérisée en ce qu'un dispositif de mesure de température (33) est prévu pour mesurer la température dans la chambre de combustion à lit fluidisé supplémentaire (12).
  4. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 3, caractérisée en ce qu'au moins un dispositif de réglage (30, 35) est prévu pour régler la quantité et/ou la teneur en oxygène d'un flux de fluide contenant de l'oxygène et/ou de l'air et/ou de la vapeur et/ou du CO2. injecté dans la chambre de combustion à lit fluidisé supplémentaire (12) par l'intermédiaire de l'au moins un dispositif d'alimentation (27, 28).
  5. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 4, caractérisée en ce que le dispositif de réglage est en liaison fonctionnelle avec le dispositif de mesure de température (33) pour régler la quantité et/ou la teneur en oxygène du flux de fluide contenant de l'oxygène et/ou de l'air et/ou de la vapeur et/ou du CO2 injecté dans la chambre de combustion à lit fluidisé supplémentaire (12) par l'intermédiaire de l'au moins un dispositif d'alimentation (27, 28) en fonction de la température mesurée dans la chambre de combustion supplémentaire (12).
  6. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 5, caractérisée en ce que le dispositif d'alimentation (27, 28) comprend au moins une buse, de préférence une buse multi-combustible, pour l'injection d'un mélange de fluide d'au moins deux fluides oxydants différents dans la chambre de combustion supplémentaire (12).
  7. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 6, caractérisée en ce que le dispositif d'alimentation (27, 28) est associé à au moins une vanne (30, 35) d'arrêt et/ou de régulation du flux de fluide oxydant et/ou fluidifiant alimenté.
  8. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 7, caractérisée en ce qu'elle comprend au moins deux dispositifs d'alimentation (27, 28) pour l'alimentation de flux de fluides oxydants de composition différente, chaque dispositif d'alimentation étant respectivement associé à au moins une vanne (30, 35) d'arrêt et/ou de régulation du flux de fluide oxydant alimenté respectif.
  9. Installation de conversion de combustibles carbonés en gaz de synthèse selon l'une des revendications 1 à 8, caractérisée en ce que
    - celle-ci comprend au moins un moyen de mesure de différence de pression (34) et un moyen d'affichage pour mesurer et afficher une différence de pression entre la pression dans la zone de lit fluidisé (11) du réacteur de gazéification (10) et la pression dans la chambre de combustion à lit fluidisé supplémentaire (12) ; et/ou
    - au moins une conduite de liaison (29) est prévue pour la recirculation du gaz brut du réacteur de gazéification (10), laquelle ramène au moins des parties du flux de gaz brut généré dans la chambre de combustion à lit fluidisé supplémentaire (12) ; et/ou
    - au moins un compresseur est prévu pour comprimer le gaz brut recirculé du réacteur de gazéification (10) dans la chambre de combustion à lit fluidisé supplémentaire (12).
  10. Procédé de conversion de combustibles carbonés en gaz de synthèse, les combustibles étant gazéifiés au moyen d'un agent de gazéification approprié dans un réacteur de gazéification (10) avec au moins une zone de lit fluidisé (11), un flux de cendres carbonées étant obtenu comme produit de fond dans une région de fond sous la zone de lit fluidisé (11) et un dispositif étant disposé sous le réacteur de gazéification (10), dans lequel le produit de fond est oxydé au moyen d'une alimentation en agent oxydant, caractérisé en ce que
    - le produit de fond est oxydé dans une chambre de combustion à lit fluidisé supplémentaire (12) disposée sous la zone de lit fluidisé (11) du réacteur de gazéification (10), et
    - un flux de fluide oxydant est injecté dans la chambre de combustion à lit fluidisé supplémentaire (12) par l'intermédiaire d'au moins un premier dispositif d'alimentation (27), lequel flux de fluide contient de l'oxygène et/ou de l'air et/ou de la vapeur, et un flux de fluide est injecté dans la chambre de combustion à lit fluidisé supplémentaire (12) par l'intermédiaire d'au moins un second dispositif d'alimentation (28), lequel flux de fluide contient du CO2 et/ou du gaz recyclé du réacteur de gazéification (10).
  11. Procédé selon la revendication 10, caractérisé en ce que le gaz de combustion résultant de l'oxydation du produit de fond dans la chambre de combustion à lit fluidisé supplémentaire (12) est introduit par la partie inférieure dans le réacteur de gazéification (10) et sert à fluidifier les particules à gazéifier.
  12. Procédé selon l'une des revendications 10 ou 11, caractérisé en ce qu'une partie du gaz brut généré lors de la gazéification dans le réacteur de gazéification (10) est recirculée du réacteur de gazéification dans la chambre de combustion à lit fluidisé supplémentaire (12) par l'intermédiaire d'au moins une conduite de liaison (29).
  13. Procédé selon la revendication 12, caractérisé en ce que la partie recirculée du gaz brut généré lors de la gazéification dans le réacteur de gazéification (10) est comprimée au moyen d'au moins un compresseur avant d'être introduite dans la chambre de combustion à lit fluidisé supplémentaire (12).
  14. Procédé selon l'une des revendications 12 ou 13, caractérisé en ce que la vitesse de sortie du produit de fond du réacteur de gazéification (10) dans la chambre de combustion à lit fluidisé supplémentaire (12) située en dessous de celui-ci est ajustée, de préférence à l'aide du flux du gaz recirculé, de telle sorte que seules des particules grossières passent du réacteur de gazéification (10) à la chambre de combustion à lit fluidisé supplémentaire (12) située en dessous de celui-ci en raison de la gravité.
  15. Procédé selon l'une des revendications 10 à 14, caractérisé en ce que
    - la gazéification des combustibles dans le réacteur de gazéification (10) s'effectue à une pression de service d'au moins environ 10 bars ; et/ou
    - la température dans la chambre de combustion à lit fluidisé supplémentaire (12) est mesurée et la teneur en oxygène de l'agent oxydant alimenté dans la chambre de combustion à lit fluidisé (12) est ajustée en conséquence en fonction de la température mesurée.
EP17811206.6A 2016-11-24 2017-11-15 Procédé et appareil de réduction de carbone dans le produit inférieur d'un gazéificateur à lit fluidisé Active EP3548587B1 (fr)

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PL17811206T PL3548587T3 (pl) 2016-11-24 2017-11-15 Sposób i urządzenie do redukcji węgla w dennym produkcie reaktora zgazowującego z fluidalnym złożem

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DE102016223318.1A DE102016223318A1 (de) 2016-11-24 2016-11-24 Verfahren und Anlage zur Kohlenstoff-Reduzierung im Bodenprodukt eines Wirbelschichtvergasers
PCT/EP2017/079320 WO2018095781A1 (fr) 2016-11-24 2017-11-15 Procédé et système pour la réduction du carbone dans la fraction de queue d'un gazéificateur à lit fluidisé

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CN111718764B (zh) * 2020-07-29 2022-01-25 山东百川同创能源有限公司 一种气化炉灰渣残炭燃烧及冷却系统和方法
ES2965008T3 (es) 2021-01-06 2024-04-10 Gidara Energy B V Proceso para producir gas de síntesis a través de conversión termoquímica de biomasa y materiales residuales
EP4293093A1 (fr) * 2022-06-15 2023-12-20 GIDARA Energy B.V. Procédé et installation de traitement destinés à la conversion de la charge d'alimentation comprenant un combustible solide contenant du carbone

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JPS5776088A (en) * 1980-10-31 1982-05-12 Nippon Kokan Kk <Nkk> Coal gasification using powdered coal and its device
JPS58225191A (ja) * 1982-06-24 1983-12-27 Nippon Kokan Kk <Nkk> 流動層による石炭のガス化方法及びその装置
DE4339973C1 (de) * 1993-11-24 1995-07-13 Rheinische Braunkohlenw Ag Verfahren zur Vergasung von Abfallstoffen
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
DE102007006982B4 (de) * 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102012016086A1 (de) 2012-08-14 2014-02-20 Thyssenkrupp Uhde Gmbh Vorrichtung und Verfahren zur Eindüsung von Sauerstoff in eine druckaufgeladene Wirbelschichtvergasung
DE102013107311A1 (de) 2013-07-10 2015-01-15 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur Nachbehandlung des bei der Vergasung anfallenden C-haltigen Bodenproduktes

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PL3548587T3 (pl) 2021-10-18
ES2877770T3 (es) 2021-11-17
EP3548587A1 (fr) 2019-10-09
DE102016223318A1 (de) 2018-05-24
PT3548587T (pt) 2021-06-24
DK3548587T3 (da) 2021-06-21

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