JP6693345B2 - Tar reformer - Google Patents

Description

  The present disclosure relates to a tar reforming apparatus that reforms tar in synthesis gas.

  In recent years, a technology has been developed in which raw materials such as coal, biomass, and unused fuels such as tire chips are gasified instead of petroleum to generate synthesis gas. The synthesis gas thus generated is used in a power generation system, hydrogen production, synthetic fuel (synthetic petroleum) production, chemical fertilizer (urea) production, and other chemical products production. Among synthetic gas raw materials, coal has a useful life of about 100 years, which is more than twice that of petroleum. In addition, coal has less uneven reserves than oil. Therefore, coal is expected as a natural resource that can be stably supplied over a long period of time.

  Conventionally, the gasification process of coal has been performed by partial oxidation using oxygen or air. However, conventional gasification processes require partial oxidation at high temperatures such as 2000 ° C. Therefore, the conventional gasification process has a drawback that the cost of the gasification furnace is high.

  In order to solve this problem, a technology (steam gasification) that uses steam to gasify coal at about 700 ° C to 900 ° C has been developed. In this steam gasification technology, the cost can be reduced by setting the temperature low. However, the produced synthesis gas contains more tar than the synthesis gas produced by partial oxidation at a high temperature of 2000 ° C. For this reason, when the temperature of the synthesis gas decreases in the process that utilizes the synthesis gas generated by steam gasification, the tar contained in the synthesis gas condenses, clogging of the pipes, failure of equipment used in the process, and catalyst damage. Problems such as poison will occur.

  Therefore, a technique has been developed in which the tar contained in the synthesis gas is removed by bringing the synthesis gas into contact with the catalyst and reforming the tar with the catalyst (for example, Patent Document 1). In the technique of Patent Document 1, in order to raise the synthesis gas to the activation temperature of the catalyst, an oxidizing agent is supplied to the synthesis gas to burn a part of the synthesis gas.

JP, 2014-205582, A

  In the technique of Patent Document 1 described above, soot may be generated from hydrocarbons and tar in the synthesis gas when the synthesis gas and the oxidant react with each other. In this case, the soot causes troubles in the operation of the equipment.

  In view of such a problem, the present disclosure aims to provide a tar reformer capable of reducing the amount of soot generated.

  In order to solve the above-mentioned problems, a tar reforming apparatus is connected to a first flow path and a second flow path through which a synthesis gas passes, and a synthesis gas introduced from the first flow path. A combustor for combusting the above with an oxidant having a stoichiometric ratio or more, the combustor, and the second flow path, and a confluent portion into which the combustion exhaust gas generated in the combustor and the synthesis gas are introduced. And a catalyst part for holding a catalyst for reforming tar contained in a mixed gas of the combustion exhaust gas and the synthesis gas generated in the confluence part, and introducing the mixed gas.

  Also, an adjusting unit is provided for adjusting the flow rate of the synthetic gas passing through the first flow path and the flow rate of the synthetic gas passing through the second flow path, based on the temperature of the mixed gas at the inlet of the catalyst section. May be.

  It is possible to reduce the amount of soot generated.

It is a figure for demonstrating a synthesis gas generator. It is a figure for explaining a tar reforming device. It is the III-III sectional view taken on the line of FIG.

  Embodiments will be described in detail below with reference to the accompanying drawings. The dimensions, materials, and other specific numerical values shown in the embodiments are merely examples for facilitating understanding, and do not limit the present disclosure unless otherwise specified. In this specification and the drawings, elements having substantially the same function and configuration are denoted by the same reference numerals to omit redundant description, and elements not directly related to the present disclosure are omitted. To do.

(Syngas generator 100)
FIG. 1 is a diagram for explaining a synthesis gas generation device 100. As shown in FIG. 1, the synthesis gas generation device 100 includes a combustion furnace 112, a medium separation device (cyclone) 114, a gasification furnace 116, a tar reforming device 200, and a refining device 300. It In FIG. 1, the flow of raw material is shown by a dashed arrow, the flow of gas is shown by a solid arrow, and the flow of a fluid medium (sand) is shown by an alternate long and short dash line.

In the synthesis gas generation device 100, as a whole, a fluid medium composed of sand such as silica sand (silica sand) having a particle size of about 300 μm is circulated as a heat medium. Specifically, first, the fluidized medium is heated to about 900 ° C. to 1000 ° C. in the combustion furnace 112. The fluidized medium heated in the combustion furnace 112 is introduced into the medium separation device 114 together with the combustion exhaust gas containing carbon dioxide (CO ₂ ). In the medium separation device 114, the high temperature fluid medium and the combustion exhaust gas are separated. The separated high-temperature fluidized medium is introduced into the gasification furnace 116. Then, the fluidized medium introduced into the gasification furnace 116 is fluidized by the gasifying agent (steam) introduced from the bottom surface of the gasification furnace 116, and finally returned to the combustion furnace 112. Further, the combustion exhaust gas separated by the medium separation device 114 is subjected to heat recovery by a boiler or the like.

  The gasification furnace 116 is, for example, a bubbling fluidized bed gasification furnace which is a type of a circulating fluidized bed system. The gasification furnace 116 gasifies the raw material at 700 ° C. to 900 ° C. to generate synthesis gas. The raw material is, for example, solid raw material such as coal such as brown coal, petroleum coke (petro coke), biomass, tire chips, or liquid raw material such as black liquor. In the present embodiment, by supplying steam to the gasification furnace 116, the raw material is gasified to generate synthesis gas (steam gasification).

  Here, the gasification furnace 116 will be described by taking a circulating fluidized bed system as an example. However, the structure of the gasification furnace 116 is not limited as long as the raw material can be gasified. For example, the gasification furnace 116 may be a simple bubbling fluidized bed system or a moving bed system in which sand moves down vertically by its own weight to form a moving bed.

  The synthesis gas GG1 generated in the gasification furnace 116 contains tar, water vapor and the like. Therefore, the synthesis gas GG1 is introduced into the tar reforming apparatus 200 described later, and the tar is reformed by the tar reforming apparatus 200. The synthesis gas GG2 whose tar has been reformed in the tar reforming apparatus 200 is further refined in the purifying apparatus 300. Further, the char (raw material residue) produced in the gasification furnace 116 is introduced into the combustion furnace 112 together with the fluidized medium, and is burned in the combustion furnace 112.

  The purification device 300 includes a heat exchanger, a spray tower, a mist separator, a booster, a desulfurization device, a denitration device, a desalination device, etc., and purifies the synthesis gas GG2. The heat exchanger cools the synthesis gas GG2 sent from the tar reformer 200. The spray tower sprays water onto the syngas cooled by the heat exchanger to remove residual tar and sludge. The mist separator sprays synthetic gas with mist-like water to further remove residual tar and sludge. The booster boosts the synthesis gas from which residual tar and sludge have been removed. A desulfurizer removes sulfides from syngas. The denitration device removes nitride from the syngas. The desalination device removes chloride from the syngas.

(Tar reformer 200)
Subsequently, a specific configuration of the tar reforming apparatus 200 will be described. FIG. 2 is a diagram for explaining the tar reforming apparatus 200. In the following drawings including FIG. 2 of the present embodiment, the X axis (horizontal direction), the Y axis (horizontal direction), and the Z axis (vertical direction) that intersect vertically are defined as illustrated. Further, in FIG. 2, the synthetic gas GG1 generated in the gasification furnace 116 is indicated by a black arrow, the oxidizer SZ is indicated by a dashed arrow, the combustion exhaust gas NG is indicated by a hatching arrow, and is synthesized with the combustion exhaust gas NG. The mixed gas KG with the gas GG1 is shown by a cross-hatched arrow, and the tar-reformed synthesis gas GG2 contained in the synthesis gas GG1 is shown by an outline arrow.

  As shown in FIG. 2, the tar reforming apparatus 200 includes a reforming furnace 210, a main pipe 310, a branch pipe 320, an oxidant supply unit 330, and an adjusting unit 340.

  The reforming furnace 210 includes a cylindrical outer wall portion 212, an upper wall portion 214 that seals the upper surface of the outer wall portion 212, and a lower wall portion 216 that seals the lower surface of the outer wall portion 212. The reforming furnace 210 is installed so that the axis of the outer wall portion 212 is in the vertical direction (Z-axis direction in FIG. 2).

  The internal space of the reforming furnace 210 is divided into three regions (combustion part 240 in order from the top, by the first protrusion 220 and the second protrusion 230, which are ring-shaped members protruding from the inner peripheral surface of the outer wall 212. It is divided into a merging section 250 and a catalyst section 260). The merging portion 250 is communicated with the combustion portion 240 via the passage 270. The catalyst portion 260 is communicated with the merging portion 250 via the passage 272. Hereinafter, the merging section 250, the combustion section 240, and the catalyst section 260 will be described in this order.

  A main inlet 252 is formed in the outer wall portion 212 forming the confluence portion 250, and the main pipe 310 is connected to the main inlet 252. The main pipe (second flow path) 310 connects the gasification furnace 116 and the confluence part 250. Therefore, the synthesis gas GG1 is introduced from the gasification furnace 116 to the confluence section 250 through the main pipe 310. Further, as will be described later in detail, the combustion exhaust gas NG is introduced into the confluence portion 250 through the passage 270. Therefore, in the merging part 250, the mixed gas KG of the synthesis gas GG1 and the combustion exhaust gas NG is generated.

  A sub-inlet 242 is formed in the outer wall 212 that constitutes the combustion section 240. A branch pipe (first flow path) 320 is connected to the sub inlet 242. The branch pipe 320 is a pipe branched from the main pipe 310. In other words, the branch pipe 320 connects the gasification furnace 116 and the combustion section 240. Therefore, the synthesis gas GG1 is introduced from the gasification furnace 116 to the combustion section 240 through the branch pipe 320.

  The oxidant supply part 330 supplies the oxidant SZ into the combustion part 240 through the oxidant supply port 332 formed in the upper wall part 214. The oxidant supply port 332 is formed substantially in the center of the upper wall portion 214 (combustion portion 240). In the present embodiment, the oxidant supply port 332 is designed so that the oxidant SZ is supplied from the direction orthogonal to the swirling flow of the synthesis gas GG1. Further, the oxidant supply unit 330 supplies the oxidant SZ having a flow rate smaller than the flow rate of the synthetic gas GG1 introduced from the branch pipe 320 to the combustion unit 240.

  In the present embodiment, the oxidant supply unit 330 supplies the oxidant SZ (for example, oxygen) having a stoichiometric ratio or higher to the combustion unit 240 with respect to the synthesis gas GG1 introduced into the combustion unit 240 from the branch pipe 320. .. That is, the oxidant supply unit 330 converts (oxidizes) the oxidant SZ having a theoretical mixing ratio (stoichiometric mixing ratio, stoichiometric mixing ratio) or more with respect to the synthesis gas GG1, that is, the synthesis gas GG1 into carbon dioxide. ) Is supplied to the combustion section 240 in an amount equal to or more than the minimum amount required for the above. Thereby, the synthesis gas GG1 can be completely burned. Therefore, the combustion part 240 can generate the high-temperature combustion exhaust gas NG without generating soot.

  FIG. 3 is a sectional view taken along the line III-III in FIG. In FIG. 3, the synthetic gas GG1 is shown by a black arrow. As shown in FIG. 3, the outer wall portion 212 has a substantially circular horizontal cross section. Further, the sub inlet 242 is opened at an angle from the center of the outer wall portion 212 to the inner peripheral surface side so that the synthetic gas GG1 flows along the tangential direction of the outer wall portion 212 or along the inner peripheral surface. In other words, the opening position of the sub inlet 242 is set so that the synthesis gas GG1 swirls at a high speed in the combustion section 240. Therefore, the synthesis gas GG1 guided from the gasification furnace 116 to the combustion section 240 swirls in the combustion section 240.

  Therefore, the synthesis gas GG1 guided from the gasification furnace 116 to the combustion unit 240 swirls in the combustion unit 240 and is mixed with the oxidant SZ supplied through the oxidant supply port 332 in the swirling process of the synthesis gas GG1. It

  Here, as a mixing device of the synthesis gas GG1 and the oxidant SZ, a configuration (hereinafter referred to as a comparative example) that supplies the oxidant SZ along the flow direction of the synthesis gas GG1 (for example, in the branch pipe 320). Conceivable. However, since the difference in the flow rate (momentum) between the synthesis gas GG1 and the oxidizing agent SZ is large, in the comparative example, the mixing due to the diffusion of the oxidizing agent SZ becomes dominant. Therefore, even if the oxidant supply unit 330 supplies the stoichiometric ratio of the oxidizer SZ, soot is generated due to nonuniformity due to insufficient mixing.

  On the other hand, in the configuration of the present embodiment in which the oxidant SZ is mixed in the swirling process of the synthetic gas GG1, it is possible to generate a large turbulence by making the oxidant SZ blown at a high speed and the synthetic gas GG1 orthogonal to each other. As a result, the synthesis gas GG1 and the oxidizer SZ can be rapidly mixed (the mixing distance can be shortened), as compared with the comparative example. Therefore, it is possible to suppress the local generation of a high temperature field and reduce the generation of soot.

  Further, due to the swirling of the synthesis gas GG1, a reverse flow from the downstream to the upstream is generated, and the mixing of the synthesis gas GG1 and the oxidizer SZ can be further promoted. In this way, the synthesis gas GG1 and the oxidizer SZ are evenly (uniformly) mixed.

  As a result, even if the oxidizing agent supply unit 330 supplies the stoichiometric ratio of the oxidizing agent SZ, it is possible to avoid a situation where the synthesis gas GG1 and the oxidizing agent SZ cause a poor mixing in the combustion section 240. In other words, even when the minimum necessary (stoichiometric ratio) oxidant SZ is supplied to the combustion section 240, the generation of soot is reduced by mixing the synthesis gas GG1 and the oxidizer SZ evenly. be able to.

  Further, in the configuration of the present embodiment in which the oxidant SZ is mixed in the swirling process of the synthetic gas GG1, unlike the comparative example, a plurality of oxidant supply ports 332 can be provided. Therefore, it becomes possible to mix the synthesis gas GG1 and the oxidizing agent SZ in a wide range. Thereby, the synthesis gas GG1 and the oxidizer SZ can be mixed uniformly.

  Therefore, the combustion reaction between the synthesis gas GG1 and the oxidant SZ can be promoted substantially uniformly, and the combustion exhaust gas NG can be generated with almost no soot generation. Then, the combustion exhaust gas NG generated in the combustion section 240 is introduced into the confluence section 250 via the passage 270.

  Returning to FIG. 2, the combustion exhaust gas NG generated in the combustion section 240 has a higher temperature than the synthesis gas GG1 (for example, the synthesis gas GG1 is about 800 ° C. and the combustion exhaust gas NG is about 1200 ° C.). Therefore, the temperature of the synthesis gas GG1 (the temperature of the mixed gas KG) can be increased by mixing the synthesis gas GG1 and the combustion exhaust gas NG in the confluence section 250. As will be described later in detail, the temperature of the mixed gas KG (mixed gas KG at the inlet of the catalyst section 260) generated in the merging section 250 by the adjusting section 340 is equal to the activation temperature of the catalyst held by the catalyst section 260 (for example, , 850 ° C. to 900 ° C.).

  Further, the combustion exhaust gas NG is a gas generated as a result of the complete combustion of the synthesis gas GG1, and therefore contains almost no soot. Therefore, by the configuration in which the combustion exhaust gas NG and the synthesis gas GG1 are mixed, it is possible to generate the high-temperature synthesis gas GG1 (mixed gas KG) that contains almost no soot.

  The adjustment unit 340 includes a first flow rate adjustment unit 342, a second flow rate adjustment unit 344, a flow meter 346, and a control unit 348.

  The first flow rate adjusting unit 342 is provided between the branch point of the branch pipe 320 in the main pipe 310 and the main inlet 252. The second flow rate adjusting unit 344 is provided in the branch pipe 320. The first flow rate adjusting unit 342 and the second flow rate adjusting unit 344 are composed of dampers. Therefore, it is possible to reduce the risk that the first flow rate adjustment unit 342 and the second flow rate adjustment unit 344 are broken by dust (the fluidized medium from the gasification furnace 116 that has passed through the medium separation device 114). Further, it becomes possible to reduce the maintenance frequency of the first flow rate adjusting unit 342 and the second flow rate adjusting unit 344.

  The flow meter 346 measures the flow rate of the synthetic gas GG1 flowing through the branch pipe 320 (specifically, the downstream side of the second flow rate adjusting unit 344 in the branch pipe 320).

  The control unit 348 is composed of a semiconductor integrated circuit including a CPU (central processing unit). The control unit 348 reads a program and parameters for operating the CPU itself from the ROM, and cooperates with the RAM as a work area and other electronic circuits.

  The control unit 348 controls the first flow rate adjusting unit 342 to adjust the opening degree of the main pipe 310. That is, the control unit 348 adjusts the flow rate of the synthesis gas GG1 introduced into the merging unit 250. Further, the control unit 348 controls the second flow rate adjustment unit 344 to adjust the opening degree of the branch pipe 320. That is, the control unit 348 adjusts the flow rate of the synthetic gas GG1 introduced into the combustion unit 240.

  In the present embodiment, the control unit 348 determines that the temperature of the mixed gas KG at the inlet of the catalyst unit 260 (the outlet of the merging unit 250) is equal to or higher than the activation temperature of the catalyst based on the temperature of the synthesis gas GG1 introduced into the main pipe 310. The first flow rate adjusting unit 342 and the second flow rate adjusting unit 344 are controlled so that the temperature becomes lower than the deterioration temperature. In other words, the control unit 348 controls the flow rate of the synthetic gas GG1 introduced into the merging unit 250 and the combustion unit 240 so that the temperature of the mixed gas KG at the inlet of the catalyst unit 260 becomes equal to or higher than the activation temperature of the catalyst and lower than the deterioration temperature. The flow rate of the synthetic gas GG1 to be introduced is adjusted.

  Then, the control unit 348 causes the oxidant supply unit 330 to supply the oxidizer to the combustion unit 240 based on the flow rate of the synthesis gas GG1 measured by the flow meter 346, that is, the flow rate of the synthesis gas GG1 to be introduced into the combustion unit 240. Adjust the amount of SZ.

  With the configuration including the adjustment unit 340, the temperature of the mixed gas KG at the inlet of the catalyst unit 260 can be set to be equal to or higher than the activation temperature of the catalyst and lower than the deterioration temperature. Further, the synthesis gas GG1 can be surely completely burned in the combustion section 240.

  The first projecting portion 220 arranged between the combusting portion 240 and the merging portion 250 is a ring-shaped member provided between the sub inlet 242 and the main inlet 252 on the inner peripheral surface of the outer wall portion 212. .. The first protruding portion 220 has a narrowed portion 222a that gradually reduces the flow passage cross-sectional area from the upper wall portion 214 toward the lower wall portion 216 (merging portion 250), and a flow passage from the narrowed portion 222a toward the lower wall portion 216. It is configured to include a top portion 222b having a substantially constant cross-sectional area and an enlarged portion 222c that gradually increases the flow passage cross-sectional area from the top portion 222b to the lower wall portion 216.

  With the configuration including the first protrusion 220, the mixture KK of the synthesis gas GG1 and the oxidizer SZ can be recirculated in the enlarged portion 222c. Therefore, it becomes possible to promote the mixing of the synthesis gas GG1 and the oxidant SZ in the air-fuel mixture KK (to reduce the bias of the oxidant SZ in the air-fuel mixture KK). Therefore, the combustion reaction between the synthesis gas GG1 and the oxidant SZ in the air-fuel mixture KK can be promoted substantially uniformly, soot generation can be prevented, and the combustion exhaust gas NG can be generated.

  The second protrusion 230 arranged between the confluence part 250 and the catalyst part 260 is a ring-shaped member provided between the main inlet 252 and the lower wall part 216 on the inner peripheral surface of the outer wall part 212. .. The second projecting portion 230 has a narrowed portion 232a that gradually reduces the flow passage cross-sectional area from the upper wall portion 214 (merging portion 250) toward the lower wall portion 216 (catalyst portion 260), and the narrowed portion 232a to the lower wall portion 216. It is configured to include a top portion 232b having a substantially constant flow passage cross-sectional area toward the front and an enlarged portion 232c that gradually increases the flow passage cross-sectional area from the top portion 232b toward the lower wall portion 216.

  With the configuration including the second protrusion 230, the mixed gas KG can be recirculated in the expansion portion 232c, and the mixed gas KG can be rapidly diffused below the expansion portion 232c. Therefore, it becomes possible to promote the mixing of the synthesis gas GG1 and the combustion exhaust gas NG in the mixed gas KG. Therefore, it becomes possible to make the temperature of the mixed gas KG substantially uniform.

  The catalyst unit 260 holds a catalyst that promotes reforming of tar. Here, the catalyst is configured to include at least Ni (nickel). The catalyst can reform the tar in the mixed gas KG by coming into contact with the mixed gas KG in the environment (atmosphere) of the activation temperature.

  In this way, the synthesis gas GG2 in which the tar has been reformed (removed) by the catalyst unit 260 is supplied to the purification device 300 through the outlet 218 provided in the outer wall 212 near the lower wall 216.

  As described above, according to the tar reforming apparatus 200 according to the present embodiment, by burning the synthesis gas GG1 with the oxidizer SZ having a stoichiometric ratio or higher, high temperature combustion exhaust gas NG containing no soot is generated. can do. It is possible to raise the temperature of the synthesis gas GG1 to the activation temperature of the catalyst while preventing the generation of soot with a simple configuration in which the combustion exhaust gas NG thus generated and the synthesis gas GG1 are simply mixed. Therefore, it is possible to reform and remove tar contained in the synthesis gas GG1 while avoiding a situation in which the flow passages formed between the catalysts, the pipes, the devices constituting the purification device 300, and the like are blocked by soot. You can

Further, as described above, since the gasification furnace 116 performs steam gasification, the synthesis gas GG1 generated in the gasification furnace 116 contains a large amount of steam (for example, about 50%). Therefore, by bringing the catalyst into contact with the synthesis gas GG1, it is possible to cause the tar in the mixed gas KG and the water vapor to react with each other, and to reform the tar into hydrogen (H ₂ ) and carbon monoxide (CO). Is possible.

  Although the embodiments have been described with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the embodiments. It is obvious to those skilled in the art that various changes or modifications can be conceived within the scope of the claims, and it is understood that those modifications also belong to the technical scope.

  For example, in the above-described embodiment, the gasification furnace 116 is described as an example of the supply source of the synthesis gas GG1. However, the source of the synthesis gas GG1 is not limited as long as it is the source of the synthesis gas GG1 containing tar.

  Further, in the above embodiment, the case where the first flow path for introducing the synthetic gas GG1 to the combustion section 240 is configured by the branch pipe 320 branched from the main pipe 310 has been described as an example. However, it suffices for the first flow path to be able to introduce the synthesis gas GG1 into the combustion section 240. For example, a pipe that directly connects the gasification furnace 116 and the combustion unit 240 may be used. That is, a pipe (first flow passage) that connects the gasification furnace 116 and the combustion unit 240 to each other and a pipe (second flow passage) that connects the gasification furnace 116 and the confluence unit 250 may be separately provided. ..

  Further, in the combustion unit 240 of the above embodiment, the configuration in which the synthetic gas GG1 and the oxidant SZ are mixed in the swirling process of the synthetic gas GG1 has been described. However, the mixing device for the synthesis gas GG1 and the oxidizing agent SZ is not limited. For example, both may be mixed by supplying the oxidizing agent SZ against the flow of the synthesis gas GG1. In this configuration, a plurality of supply ports for the oxidant SZ can be provided.

  Further, in the above embodiment, the configuration including the adjusting unit 340 has been described as an example. However, when the temperature of the synthesis gas GG1 introduced from the gasification furnace 116 is maintained within the predetermined temperature range, the adjusting unit 340 can be omitted. In this case, the flow passage cross-sectional areas of the main pipe 310 and the branch pipe 320 may be designed so that the temperature of the inlet of the catalyst portion 260 becomes the activation temperature of the catalyst.

  Further, in the above-described embodiment, the case where the first flow rate adjusting unit 342 and the second flow rate adjusting unit 344 are configured by dampers has been described as an example. However, the first flow rate adjusting unit 342 only needs to be able to adjust the flow rate of the second flow path. Further, the second flow rate adjusting unit 344 only needs to be able to adjust the flow rate of the first flow path. For example, the first flow rate adjusting unit 342 and the second flow rate adjusting unit 344 may be configured by a fan or a pump.

  Further, in the above-described embodiment, the catalyst including at least Ni is described as an example. However, the material of the catalyst is not limited as long as the tar in the mixed gas can be modified to remove the tar. For example, an oxide or carbonate of one or more elements selected from the group of Ca (calcium), Mg (magnesium), Fe (iron), and Si (silicon), for example, dolomite, olivine, Natural ores such as limonite and limestone may be used as the catalyst. That is, a catalyst containing one or more selected from the group of Ca, Mg, Fe, and Si may be adopted.

  The present disclosure can be used for a tar reforming device that reforms tar in synthesis gas.

200 Tar reformer 240 Combustion section 250 Confluence section 260 Catalyst section 310 Main pipe (second flow path)
320 Branch pipe (first flow path)
340 Adjuster

Claims (2)

A first channel and a second channel through which the synthesis gas passes,
A combustor connected to the first channel for combusting the synthesis gas introduced from the first channel with an oxidizer having a stoichiometric ratio or higher;
A confluence part connected to the combustion part and the second flow path, into which a combustion exhaust gas generated in the combustion part and the synthesis gas are introduced,
Holding a catalyst for reforming tar contained in a mixed gas of the combustion exhaust gas and the synthesis gas generated in the confluence section, and a catalyst section into which the mixed gas is introduced,
Tar reformer equipped with.   An adjusting unit for adjusting the flow rate of the synthetic gas passing through the first flow path and the flow rate of the synthetic gas passing through the second flow path based on the temperature of the mixed gas at the inlet of the catalyst unit. Item 1. The tar reformer according to Item 1.

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