JP2010215888A - Circulation fluidized bed gasification reactor - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a circulation fluidized bed gasification reactor which can reduce the used amount of tar adsorptive material such as porous particles used for a fluidized medium as much as possible, can circulate the fluidized medium without allowing the fluidized medium to coexist with ash particles and can reduce a cost required for tar treatment. <P>SOLUTION: The circulation fluidized bed gasification reactor is configured such that a raw material is gasified in a fluidized bed gasification furnace into which the fluidized medium is introduced, char produced upon gasification and the fluidized medium are introduced into a fluidized bed combustion furnace of a post step, an uncombusted content is combusted and the reheated fluidized medium is circulated in the reactor, wherein, on a preliminary step of the fluidized bed gasification reactor, a pyrolysis furnace of a two-step furnace structure in which a tar absorption furnace and a fuel pyrolysis furnace are disposed on upper and lower stages is disposed, and a fluidized medium which contains uncombusted char taken out of the fuel pyrolysis furnace of the lower stage and a fluidized medium to which the tar taken out of the tar absorption furnace of the upper stage is adsorbed are circulated independently. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

  The present invention relates to a gasification reactor for extracting combustible gas from fuel using a circulating fluidized bed.

Conventionally, technologies have been developed to make effective use of organic resources by using solid fuels of hydrocarbon resources such as coal, biomass, garbage, and sewage sludge, and using the generated gas as a combustible gas and heat source. Yes.
As one of the gasifiers, the reactor is separated into a fluidized bed gasification furnace and a fluidized bed combustion furnace, a solid fuel of hydrocarbon resources is supplied to the fluidized bed gasification furnace, gasified with steam, and generated There is one that uses a circulating fluidized bed in which the unburned portion (char) and the fluidized medium are combusted in a fluidized bed combustion furnace and the heated fluidized medium is returned to the gasification furnace (Patent Document 1).
The gasification reaction furnace is an external circulation system, but there is an internal circulation system such as the reaction furnace described in Patent Document 2, in which particulate slag is used as a fluid medium. As a result, the tar contained in the gas generated in the gasification furnace is reformed to generate a combustible gas with a small amount of tar, and the deteriorated slag is introduced into the combustion furnace together with unburned char and reactivated. , Returned to the gasifier.
In the circulating fluidized bed gasification system having these fluidized bed gasification furnace and fluidized bed combustion furnace, the gasification gas and the combustion gas can be separately taken out from the respective furnaces, and the high calorie does not contain an inert gas. Gas can be produced.

However, as in the inventions described in Patent Documents 1 and 2, if pyrolysis and gasification are simultaneously performed in a gasification furnace, char gasification is unlikely to occur. This is because the reaction rate is lowered by the adsorption of H ₂ gas generated during thermal decomposition on the char surface. Therefore, in order to gasify the high-content char fuel, it is necessary to perform at a high temperature or high pressure of 1200 to 1400 ° C., and a problem that an expensive catalyst such as nickel must be used at a low temperature of 800 to 900 ° C. is there.

Further, Patent Document 3 generates biomass by gasifying biomass in a gasification reaction system under heating conditions in the gasification of biomass in which biomass and a gasifying agent are introduced into a gasification furnace and converted into synthesis gas. An efficient biomass gasification method is described in which a useful synthesis gas can be obtained in a high yield by gasifying on the low temperature side without adding an expensive catalyst from the outside by effectively using ash. .
However, in the method described in Patent Document 3, after the biomass is gasified, the ash scattered outside the furnace is recovered, and the tar is reformed by passing the gas therethrough. Although it is described that it is not necessary to use an expensive catalyst in the latter stage of the furnace, it does not promote char gasification in the furnace.

Further, Patent Document 4 discloses that in a system in which a raw material is gasified in a fluidized bed furnace and pyrolyzed or partially oxidized to obtain a product gas, tar generated from the raw material is converted into a fluid catalytic cracking catalyst, a fluid catalytic cracking equilibrium catalyst, silica -It is described that tar is removed by using alumina-based particles or alumina-based particles produced by an oil immersion granulation method.
However, the method described in Patent Document 4 is a method in which tar is efficiently adsorbed by porous particles, but it is extremely expensive than the conventionally used cinnabar sand as a fluid medium, and thus costs are increased. Further, in the fluidized bed furnace, ash is extracted from the lower part of the furnace at regular intervals. However, in order to be mixed with porous particles, the porous particles must be extracted together. Therefore, the extracted amount must be newly supplied into the furnace. Therefore, the higher the ash content fuel such as coal, the higher the running cost is likely.

The present inventors have solved these problems and promoted gasification of a solid fuel containing a large amount of char at a low temperature, thereby increasing the amount of product gas that can be extracted in a gasification furnace, and a method for extracting combustible gas with high efficiency. A gasification reactor for this purpose has already been proposed. (See Patent Document 5).
This method is a method of improving the gasification efficiency by providing an alkali absorption furnace in front of the gasification furnace and actively adsorbing the alkali in the volatile gas to the char and using it as a gasification catalyst. In addition to improving the gasification efficiency of char by adsorbing tar to the char in the furnace, it is possible to avoid the effect of inhibiting the gasification of char, and from the pyrolysis gas generated from the alkali absorption furnace and the gasification furnace There is an advantage that the gasified gas to be generated is separated and taken out to increase the total amount of generated gas.

  Further, in Patent Document 6, a fluidized bed gasification furnace is provided by introducing a chamber in which an organic material is supplied and generating a pyrolysis gas containing tar by a pyrolysis reaction, and introducing a pyrolysis residue generated by the pyrolysis reaction into a gas. It is described that the generation of high-quality gasification gas is enhanced by dividing it into a chamber for generating gasification gas.

JP 2005-41959 A JP 2005-68297 A JP 2005-68373 A JP 2005-272882 A JP 2008-303377 A JP 2008-156552 A

The present inventors further examined the gasification method and apparatus using the circulating fluidized bed gasification reactor, and when a tar adsorbing substance such as alumina, limestone, or zeolite was added as a fluid medium, the tar was Although there is an advantage that it can be adsorbed efficiently, in particular, when porous particles such as porous alumina are used as the tar adsorbing substance, although tar can be adsorbed more efficiently, it is more than the conventional sand used as a fluid medium. However, it is necessary to reduce the amount of use as much as possible.
Further, as in Patent Document 4, since porous particles and ash particles coexist in the furnace, the porous particles are also extracted together when the ash is extracted from the lower part of the furnace at regular intervals.
Furthermore, it is necessary to reduce the cost (reforming furnace, scrubber, etc.) required for tar treatment at the latter stage of the furnace.

  The present invention solves such problems in the prior art, and reduces the amount of use as much as possible without mixing an expensive fluid medium with ash particles, and can reduce the cost for tar treatment. The object is to provide a reaction furnace.

  As a result of intensive research to achieve the above object, the present inventors have provided a fuel pyrolysis furnace having a two-stage furnace structure having a tar absorption furnace in the upper stage of the gasification furnace, and a lower stage fuel. The inventor has found that the fluid medium containing the unburned char taken out from the pyrolysis furnace and the fluid medium adsorbed with the tar taken out from the upper tar absorption furnace can be solved by independently circulating them.

The present invention has been completed based on these findings, and according to the present invention, the following inventions are provided.
[1] The raw material is gasified in the fluidized bed gasification furnace into which the fluidized medium is introduced, and the char and fluidized medium generated during the gasification are introduced into the subsequent fluidized bed combustion furnace to burn the unburned portion. A circulating fluidized bed gasification reactor configured to circulate the reheated fluid medium in the reactor,
In front of the fluidized bed gasification furnace, a two-stage furnace pyrolysis furnace equipped with a tar absorption furnace and a fuel pyrolysis furnace is provided, and contains unburned char taken out from the lower fuel pyrolysis furnace. A circulating fluidized bed gasification reactor, wherein the fluidized medium and the fluidized medium adsorbed with the tar taken out from the upper tar absorption furnace are circulated independently of each other.
[2] A char gasification furnace and a char residue combustion furnace are connected in this order to the subsequent stage of the lower fuel pyrolysis furnace, and a coke gasification furnace and a coke residue combustion furnace are connected in this order to the subsequent stage of the upper tar absorption furnace. The circulating fluidized bed gasification reactor according to [1] above, which is characterized in that
[3] The circulating fluidized bed gasification reactor according to [2], wherein the gasification furnace is a two-stage furnace including the char gasification furnace in the lower stage and the coke gasification furnace in the upper stage.
[4] The circulating fluidized bed gasification reactor according to [2], wherein the char gasification furnace and the coke gasification furnace are separate gasification furnaces.
[5] The circulating fluidized bed gasification reactor according to [2], wherein the char gasification furnace is omitted, and a char residue combustion furnace is directly connected to a rear stage of the lower fuel pyrolysis furnace.
[6] The circulating fluidized bed gasification reactor according to [2], wherein the coke gasification furnace is omitted, and a coke residue combustion furnace is directly connected to the rear stage of the upper tar absorption furnace.
[7] The above-mentioned upper tar absorption furnace uses a tar adsorbing substance as a fluid medium, and adsorbs the tar generated in the lower fuel pyrolysis furnace to the fluid medium. The circulating fluidized bed gasification reactor according to any one of 1] to [6].
[8] The circulating fluidized bed gasification reactor according to any one of [1] to [7], wherein the lower fuel pyrolysis furnace uses dredged sand as a fluid medium.
[9] Pyrolysis gas generated by pyrolysis of volatile matter and tar reforming in the fuel pyrolysis furnace, gasification gas generated by char and / or coke gasification in the fluidized bed gasification furnace, and The circulating fluidized bed according to any one of the above [1] to [8], comprising means for independently taking out combustion gases generated by combustion of char residue and / or coke residue in a fluidized bed combustion furnace Gasification reactor.
[10] The circulating fluidized bed gasification reactor according to any one of [1] to [9], wherein the fuel pyrolysis furnace has an alkali absorption function.

  According to the present invention, by providing a pyrolysis furnace having a two-stage furnace structure having a tar absorption furnace and a fuel pyrolysis furnace at the upper and lower stages in front of the gasification furnace, only the fluid medium of the tar absorption furnace is expensive. It is possible to use a tar-adsorbing substance, the amount of use can be minimized, and a fluid medium containing unburned char taken from the lower fuel pyrolysis furnace and an upper tar absorption furnace can be used. By circulating each of the extracted fluid media on which the tar is adsorbed independently, the expensive tar adsorbing substance and the ash particles can be prevented from being mixed, and the cost for the tar treatment can be reduced. Furthermore, in the present invention, the fuel pyrolysis furnace and the char gasification furnace are completely separated from each other and connected to each other so that the char can be efficiently gasified with a minimum amount of gasifying agent. In addition, the tar absorption furnace and the coke gasification furnace are completely separated and made stand-alone, and by connecting them, the coke can be efficiently gasified with a minimum amount of gasifying agent.

The figure which shows typically 1st Embodiment of the circulating fluidized-bed gasification reactor of this invention. The figure which shows typically 2nd Embodiment of the circulating fluidized bed gasification reactor of this invention. The figure which shows typically 3rd Embodiment of the circulating fluidized-bed gasification reactor of this invention. The figure which shows typically 4th Embodiment of the circulating fluidized-bed gasification reactor of this invention. The figure which shows typically 5th Embodiment of the circulating fluidized-bed gasification reactor of this invention. The figure which shows typically 6th Embodiment of the circulating fluidized bed gasification reactor of this invention. The figure which shows typically 7th Embodiment of the circulating fluidized-bed gasification reactor of this invention.

  Embodiments of the present invention will be described below with reference to the drawings. However, the present invention is not limited to these embodiments.

FIG. 1 is a diagram schematically showing a first embodiment of a circulating fluidized bed gasification reactor according to the present invention, which is a fuel having a two-stage furnace configuration having a tar absorption furnace and a fuel pyrolysis furnace at the top and bottom. A pyrolysis furnace, a char gasification furnace and a char residue combustion furnace are connected in this order to the lower stage of the fuel pyrolysis furnace, and a coke gasification furnace and a coke residue combustion are connected to the latter stage of the upper tar absorption furnace. The furnaces are connected in this order. The char gasification furnace and the coke gasification furnace are two-stage fluidized bed gasification furnaces provided at the lower stage and the upper stage, respectively, and the char residue combustion furnace and the coke residue combustion furnace are independent fluidized respectively. It consists of a layer combustion furnace.
In the present invention, the fuel pyrolysis furnace is a furnace having an alkali absorption function as described in Patent Document 3, and the gasification catalyst is prepared by actively adsorbing the alkali in the volatile gas to the char. Needless to say, the gasification efficiency of char can be improved.

  In the circulating fluidized bed gasification reactor shown in the figure, the fluid medium that adsorbs the tar taken out from the upper tar absorption furnace passes through the coke gasification furnace and the coke residue combustion furnace connected to the subsequent stage to the tar absorption furnace. On the other hand, the fluid medium taken out from the lower fuel pyrolysis furnace is returned to the fuel pyrolysis furnace through the char gasification furnace and the char residue combustion furnace connected to the subsequent stage.

Porous particles such as porous alumina are preferably used in order to efficiently absorb tar generated from the raw material, but have the disadvantage of being expensive.
In the circulating fluidized bed gasification reactor according to the present invention, a thermal decomposition furnace having a two-stage furnace structure having a tar absorption furnace and a fuel pyrolysis furnace at the top and bottom is provided in the upstream of the fluidized bed gasification furnace. As a fluid medium for the tar absorption furnace of the present invention, those having good tar adsorption efficiency such as porous particles are used, and the fluid medium introduced into the fuel pyrolysis furnace at the lower stage is generally used inexpensive cinnabar It is possible to minimize the amount of the expensive fluid medium used by using a material containing as a main component.
In addition, since the char residue combustion furnace and the coke residue combustion furnace are separated, fluid media such as porous particles circulating in the upper tar absorption furnace should not be mixed with the ash particles generated in the char residue combustion furnace. it can.
Further, since tar treatment can be performed in the furnace, the cost conventionally required for the tar treatment at the latter stage of the furnace can be reduced.

Hereinafter, the gasification of the raw material is performed using an example in which porous particles such as porous alumina are used for the fluid medium of the upper tar absorption furnace and dredged sand is used for the fluid medium of the lower fuel pyrolysis furnace. This will be specifically described.
A hydrocarbon-based solid fuel such as biomass, garbage, sewage sludge, and coal is supplied to the fuel pyrolysis furnace, and for example, CO ₂ gas in which a part of the generated combustion gas is circulated from the lower part, or An inert gas such as N ₂ or Ar is introduced as a flowing gas, and the above hydrocarbon solid fuel supplied to the fuel cracking furnace is pyrolyzed.
The tar generated simultaneously with the generated pyrolysis gas flows to the upper tar absorption furnace. The tar is adsorbed by the porous particles in the tar absorption furnace and partly reformed into gas. The pyrolysis gas containing no tar can be taken out from the pyrolysis gas take-out means provided at the top.
The extracted pyrolysis gas is a kind of combustible gas, and is used for power generation by a fuel cell or a gas engine, liquid fuel, and the like.
In the present invention, the raw material for gasification is not limited to the hydrocarbon-based solid fuel as described above, and a liquid fuel that easily generates tar can also be used.

In the lower fuel pyrolysis furnace, the pyrolyzed char and cinnabar are sent to the next char gasification furnace.
On the other hand, the porous particles having adsorbed tar in the upper tar absorption furnace are sent to the upper coke gasification furnace.

The char gasification furnace and the coke gasification furnace are in a two-stage fluidized bed having the respective furnaces in the lower stage and the upper stage, and the char and coke introduced into each furnace are combined with the gasifying agent introduced from the lower part. It is gasified by the gasification reaction. As the gasifying agent, water vapor, oxygen, air, or the like is used. The gasification gas produced by reacting with the gasifying agent is taken out from the upper part of the coke gasification furnace.
The extracted gasification gas is a combustible gas, and is used for power generation by a fuel cell or a gas engine, liquid fuel, or the like.

  In the apparatus shown in FIG. 1, the pyrolysis gas taken out from the upper part of the tar absorption furnace and the gasification gas taken out from the upper part of the coke gasification furnace are taken out separately. May be used after being merged after each furnace outlet, and when used as a heat source, a heat exchanger may be attached before or after the merge.

The residue char in the char gasification furnace and the residue coke in the coke gasification furnace are respectively introduced into the next residue char combustion furnace and residue coke fuel furnace provided separately.
Both the residue char combustion furnace and the residue coke combustion furnace are fluidized beds, and ensure a residence time during which the residue char and residue coke can be completely combusted. In each combustion furnace, the introduced residue char and residue coke are burned together with air or oxygen introduced from the lower part of each combustion furnace, and the combustion gas is extracted from the extraction means provided in the upper part of each furnace by a cyclone. It is taken out.
The combustion gas taken out from each combustion furnace is mainly used as a heat source, and as described above, a part of the combustion gas can be recycled to the fuel pyrolysis furnace. It can also be used as a preheating source for air or steam introduced into the gasification furnace or each combustion furnace.
On the other hand, the silica sand reheated in the char residue combustion furnace and the porous particles reheated in the coke combustion furnace are returned to the fuel pyrolysis furnace and the tar absorption furnace, respectively.
Note that the char concentration is closely related to the reaction (especially shift reaction) occurring in the gasification furnace, and if the heat balance is within the range, a part of the unburned char is recirculated, By controlling the char concentration in the gasification furnace to a concentration suitable for the reaction, for example, the H ₂ / CO ratio at the time of gasification can be controlled, and the use for liquid fuel is advantageous.
Furthermore, if the heat balance cannot be established with only the combustion heat obtained from the residue char and residue coke, the heat balance is maintained by supplying a predetermined amount of pyrolysis gas and gasification gas to each combustion furnace and burning them. It is also possible to do.

  A fuel pyrolysis furnace and a char gasification furnace, a char gasification furnace and a residue char combustion furnace, a tar absorption furnace and a coke gasification furnace, or a communication path connecting each of the coke gasification furnace and the residue coke combustion furnace is a loop seal, L-shaped Any type of material can be used as long as the material can be sealed, such as a valve or moving layer.

  As described above, in the circulating fluidized bed gasification reactor shown in FIG. 1, the flow of the fluid medium and the solid fuel introduced into the lower fuel pyrolysis furnace is as follows: fuel pyrolysis furnace → communication passage → char gasification furnace → communication Passage → Char residue combustion furnace → Cyclone (not shown) → Downcomer (not shown) → Fuel pyrolysis furnace On the other hand, the flow of the fluid medium introduced into the upper tar absorption furnace is as follows. Path → Coke gasification furnace → Communication path → Coke residue combustion furnace → Cyclone (not shown) → Downcomer (not shown) → Tar absorption furnace.

  According to the apparatus shown in FIG. 1, since the upper and lower sides of the pyrolysis furnace are separated into two stages, a fuel pyrolysis furnace and a tar absorption furnace, a fluid medium having good tar adsorption efficiency such as porous particles, for example, By supplying porous alumina only to the upper tar absorption furnace, there is an advantage that the amount of use can be minimized. Furthermore, the fluid medium can be separately circulated in a system comprising a fuel pyrolysis furnace, a char gasification furnace and a residue char combustion furnace, and a system comprising a tar absorption furnace, a coke gasification furnace and a residue coke combustion furnace. Therefore, it is possible to prevent the fluid medium having good tar adsorption efficiency such as porous particles from mixing with the ash particles.

FIG. 2 is a diagram schematically showing a second embodiment of the circulating fluidized bed gasification reactor of the present invention.
In the apparatus shown in FIG. 1, the gasification furnace has a two-stage structure in which a char gasification furnace and a coke gasification furnace are provided at the lower and upper stages, respectively, and the generated gasification gas is taken out from the upper coke gasification furnace. However, in the apparatus shown in FIG. 2, these gasification furnaces are set as separate gasification furnaces, a gasifying agent is introduced from the lower part of each gasification furnace, and the generated gasification gas is It is comprised so that it may take out from the taking-out means provided in the upper part. Except this point, it is the same as the circulating fluidized bed gasification reactor shown in FIG.

FIG. 3 is a diagram schematically showing a third embodiment of the circulating fluidized bed gasification reaction furnace, which does not have a char gasification furnace, and is provided with a char residue combustion furnace at the rear stage of the fuel pyrolysis furnace. Is the same as the circulating fluidized bed gasification reactor shown in FIG.
In the circulating fluidized bed gasification reactor of the present invention, the solid fuel to be used is a high volatile solid fuel, and the thermal balance of the system can be obtained simply by burning the pyrolysis gas and its residue without gasifying the char. In other words, if the residual char after pyrolysis is gasified, the char gasification furnace can be omitted as shown in this embodiment.

  In the circulating fluidized bed gasification reactor shown in FIG. 3, the flow of the fluid medium made of cinnabar and the solid fuel is as follows: fuel pyrolysis furnace → communication passage → char residue combustion furnace → cyclone (not shown) → downcomer (FIG. (Not shown) → Fuel pyrolysis furnace, while the flow of fluid medium consisting of porous particles is tar absorption furnace → communication path → coke gasification furnace → communication path → coke residue combustion furnace → cyclone (not shown) → down Comer (not shown) → Tar absorption furnace.

FIG. 4 is a diagram schematically showing a fourth embodiment of the circulating fluidized bed gasification reactor, which does not have a coke gasification furnace, and a coke residue combustion furnace is provided at the rear stage of the tar absorption furnace. Except for the direct connection, it is the same as the circulating fluidized bed gasification reactor shown in FIG.
In the circulating fluidized bed gasification reactor shown in FIG. 4, the flow of the fluid medium made of cinnabar and the solid fuel is a fuel pyrolysis furnace → communication passage → char gasification furnace → communication passage → char residue combustion furnace → cyclone (not shown). → downcomer (not shown) → fuel pyrolysis furnace, while the flow of fluid medium consisting of porous particles is tar absorption furnace → communication path → coke residue combustion furnace → cyclone (not shown) → down Comer (not shown) → Tar absorption furnace.

FIG. 5 is a diagram schematically showing a fifth embodiment of the circulating fluidized bed gasification reactor, which does not have a char gasification furnace and a coke gasification furnace, and has a coke after the tar absorption furnace. 1 is the same as the circulating fluidized bed gasification reactor shown in FIG. 1 except that the residue combustion furnace is directly connected and the char residue combustion furnace is directly connected to the rear stage of the fuel pyrolysis furnace.
In the circulating fluidized bed gasification reactor shown in FIG. 5, the flow of the fluid medium made of cinnabar and the solid fuel is as follows: fuel pyrolysis furnace → communication passage → char residue combustion furnace → cyclone (not shown) → downcomer (FIG. (Not shown) → fuel pyrolysis furnace, while the flow of fluid medium consisting of porous particles is: tar absorption furnace → communication path → coke residue combustion furnace → cyclone (not shown) → downcomer (not shown) → It becomes a tar absorption furnace.

1 to 5 are schematic views showing the concept of a circulating fluidized bed gasification reactor according to the present invention. Each furnace is not only a completely separated type, but also a part or all of these furnaces are integrated. For example, the inside can be a pyrolysis furnace, a gasification furnace, the outside can be a combustion furnace, or the combustion furnace can be a two-stage furnace.
FIG. 6 and FIG. 7 show an example, and in the gasification furnace, the char gasification furnace and the coke gasification furnace may be completely separated as shown in FIG. As shown in FIG. 7, in order to reduce the heat loss of both furnaces, they may be arranged in parallel with a partition wall therebetween.
It goes without saying that the combustion furnaces of both furnaces may be arranged side by side with a partition wall in order to reduce the heat loss of both furnaces as shown in FIG.

  The system in the circulating fluidized bed gasification reactor of the present invention is applied to the utilization of unused hydrocarbon resources such as biomass, garbage, sewage sludge, and, for example, hybrid gasification (cogasification) with coal and biomass. Alternatively, it can also be applied to hybrid gasification of solid fuel and liquid fuel.

Claims (10)

The raw material is gasified in the fluidized bed gasification furnace into which the fluidized medium is introduced, and the char and fluidized medium generated during the gasification are introduced into the subsequent fluidized bed combustion furnace to burn the unburned components and reheat. A circulating fluidized bed gasification reactor configured such that the fluidized medium circulated in the reactor,
In front of the fluidized bed gasification furnace, a two-stage furnace pyrolysis furnace equipped with a tar absorption furnace and a fuel pyrolysis furnace is provided, and contains unburned char taken out from the lower fuel pyrolysis furnace. A circulating fluidized bed gasification reactor, wherein the fluidized medium and the fluidized medium adsorbed with the tar taken out from the upper tar absorption furnace are circulated independently of each other.   A char gasification furnace and a char residue combustion furnace are connected in this order to the latter stage of the lower fuel pyrolysis furnace, and a coke gasification furnace and a coke residue combustion furnace are connected in this order to the latter stage of the upper tar absorption furnace. The circulating fluidized bed gasification reactor according to claim 1, wherein   The circulating fluidized bed gasification reactor according to claim 2, wherein the gasification furnace is a two-stage furnace having the char gasification furnace in the lower stage and the coke gasification furnace in the upper stage.   The circulating fluidized bed gasification reactor according to claim 2, wherein the char gasification furnace and the coke gasification furnace are respectively separate gasification furnaces.   The circulating fluidized bed gasification reactor according to claim 2, wherein the char gasification furnace is omitted, and a char residue combustion furnace is directly connected to a rear stage of the lower fuel pyrolysis furnace.   The circulating fluidized bed gasification reactor according to claim 2, wherein the coke gasification furnace is omitted, and a coke residue combustion furnace is directly connected to the rear stage of the upper tar absorption furnace.   7. The upper tar absorption furnace uses a tar adsorbing substance as a fluid medium, and the tar generated in the lower fuel pyrolysis furnace is adsorbed to the fluid medium. The circulating fluidized bed gasification reactor according to any one of the above.   The circulating fluidized-bed gasification reactor according to any one of claims 1 to 7, wherein the lower fuel pyrolysis furnace uses cinnabar as a fluid medium.   Pyrolysis gas produced by pyrolysis of volatile matter and tar reforming in the fuel pyrolysis furnace, gasification gas produced by gasification of char and / or coke in the fluidized bed gasification furnace, and fluidized bed combustion The circulating fluidized bed gasification according to any one of claims 1 to 8, further comprising means for independently taking out combustion gases generated by combustion of char residue and / or coke residue in a furnace. Reactor. The circulating fluidized bed gasification reactor according to any one of claims 1 to 9, wherein the fuel pyrolysis furnace has an alkali absorption function.

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