Gasification gas production apparatus and gasification gas production method

Abstract

To provide the gasification gas manufacturing apparatus and the manufacturing method of the gasification gas, that can reduce tar content in the gasification gas produced in a gasification furnace.SOLUTION: The gasification gas manufacturing apparatus 100 comprises: a carbonization furnace 140 for carbonizing a solid raw material with one or both of an oxygen-containing gas and a combustion exhaust gas, and a gasification furnace 130 for gasifying a carbonized solid raw material with heat of a fluidized medium. Tar can be separated from the solid raw material introduced into the gasification furnace 130 with a configuration including the dry distillation furnace 140. Therefore, the tar content in the gasification gas produced in the gasification furnace 130 can be reduced.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present disclosure relates to a gasification gas production apparatus and a method for producing gasification gas. [Background technology]

[0002] Gasification furnaces have been developed that gasify solid feedstocks using gasifying agents such as steam or carbon dioxide at low temperatures between 700°C and 900°C. In technologies that gasify solid feedstocks at these low temperatures, the tar contained in the solid feedstocks is contained in large quantities in the resulting gasified gas. Tar condenses when cooled to temperatures below 250°C. This causes tar to adhere and accumulate on equipment and piping downstream of the gasification furnace. This can lead to problems such as blockage of piping and poisoning of catalysts contained in the equipment.

[0003] As technologies for removing tar from gasification gas, wet and dry methods have been proposed. The wet method is a method in which water is sprayed onto the gasification gas to cool it, condensing the tar and separating and removing it (for example, Patent Document 1). The dry method is a method in which part of the gasification gas is partially oxidized (combusted) to raise the temperature to about 1300°C, and the tar is decomposed and removed (for example, Patent Document 2). [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Patent No. 5217292 [Patent Document 2] Patent No. 5217295 Summary of the Invention [Problem to be solved by the invention]

[0005] The wet process generates a large amount of wastewater containing tar, which increases the cost of treating the wastewater. Furthermore, the dry process results in a lower content of combustible gases (hydrogen and carbon monoxide) in the gasification gas (cold gas efficiency = chemical energy of gasification gas / chemical energy of solid raw material) compared to the wet process. Therefore, there is a need for the development of technology that can reduce the tar content in the gasification gas produced in a gasification furnace.

[0006] In view of these problems, the present disclosure aims to provide a gasification gas production apparatus and a method for producing gasification gas that are capable of reducing the tar content in the gasification gas produced in a gasification furnace. [Means for solving the problem]

[0007] In order to solve the above problems, a gasification gas production apparatus according to one aspect of the present disclosure includes a main body that accommodates a solid raw material, an oxygen-containing gas Su a gas inlet for introducing an oxygen-containing gas into the main body; The heat of reaction generated by partial oxidation of volatile components contained in solid raw materials by oxygen in the The system is equipped with a carbonization furnace that heats the solid raw material to 250°C or higher and 550°C or lower to carbonize the solid raw material, a storage tank that stores the carbonized solid raw material and a fluidized medium, and a gasification furnace that has a steam inlet that introduces steam into the storage tank and gasifies the carbonized solid raw material using the heat of the fluidized medium, and the mixture obtained by mixing the carbonized solid raw material and the fluidized medium is introduced into the storage tank of the gasification furnace. In addition, the solid raw material may be introduced into the main body of the distillation furnace from the top of the main body, and the mixture obtained by mixing the solid raw material discharged from the bottom of the main body of the distillation furnace with the fluidized medium may be introduced into the storage tank of the gasification furnace, and the gas inlet of the distillation furnace may introduce an oxygen-containing gas from the bottom of the main body, and the distillation gas may be discharged from the top of the main body of the distillation furnace.

[0008] The gasification furnace may also be provided with a combustion furnace that burns the pyrolysis gas discharged from the pyrolysis furnace to heat a fluidized medium, and the fluidized medium heated by the combustion furnace may be introduced into the gasification furnace.

[0009] The system may also be provided with a cooling section that cools the distillation gas discharged from the distillation furnace to a temperature at which tar condenses, and the gas cooled by the cooling section may be discharged together with the gasification gas produced in the gasification furnace.

[0011] The water vapor introduction section may introduce water vapor at a flow rate that allows a fluidized bed of the fluidized medium to be formed in the container vessel.

[0013] In order to solve the above problems, a method for producing a gasification gas according to one embodiment of the present disclosure includes: A carbonization furnace having a main body for accommodating a solid raw material, oxygen-containing gas The heat of reaction generated by partial oxidation of volatile components contained in solid raw materials by oxygen in the The solid raw material is heated to 250°C or higher and 550°C or lower to dry distill the solid raw material, and the dry distilled solid raw material and the bed material are mixed. but The mixture after mixing is introduced into a gasification furnace, where the dry-distilled solid raw material is gasified by the heat of the fluidized medium using steam as a gasifying agent. In addition, the solid raw material may be introduced into the main body of the carbonization furnace from the top of the main body, and the mixture obtained by mixing the solid raw material discharged from the bottom of the main body of the carbonization furnace with a fluidized medium may be introduced into the gasification furnace, an oxygen-containing gas may be introduced from the bottom of the main body of the carbonization furnace, and carbonization gas may be discharged from the top of the main body of the carbonization furnace. [Effects of the Invention]

[0014] According to the present disclosure, it is possible to reduce the tar content in the gasification gas produced in the gasification furnace. [Brief explanation of the drawings]

[0015] [Figure 1] FIG. 1 is a diagram illustrating a gasification gas production apparatus. [Figure 2] FIG. 2 is a diagram illustrating a refining device. [Figure 3] 1 is a flowchart illustrating a process flow of a method for producing gasification gas. [Figure 4] FIG. 10 is a diagram illustrating a modified example of a gasification gas production apparatus. [Figure 5] FIG. 1 is a diagram showing the results of thermogravimetric differential thermal analysis of lignite. DETAILED DESCRIPTION OF THE INVENTION

[0016] Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. Dimensions, materials, and other specific numerical values ​​shown in the embodiments are merely examples for ease of understanding and do not limit the present disclosure unless otherwise specified. In this specification and drawings, elements having substantially the same functions and configurations are designated by the same reference numerals to avoid redundant explanation, and elements not directly related to the present disclosure are not shown.

[0017] Fig. 1 is a diagram illustrating a gasification gas production apparatus 100. As shown in Fig. 1, the gasification gas production apparatus 100 includes a combustion furnace 110, a first pipe 112, a second pipe 114, a cyclone 120, a third pipe 122, a gasification furnace 130, a fourth pipe 136, a dry distillation furnace 140, a fifth pipe 150, a sixth pipe 152, and a purification device 210. In Fig. 1, the flow of solids (bed material, solid raw material, residue) is indicated by solid arrows, and the flow of gases (gasification gas, combustion exhaust gas, dry distillation gas, steam, air) is indicated by dashed arrows.

[0018] The gasification gas production apparatus 100 uses a fluidized bed of a fluidized medium to gasify a solid raw material and produce gasification gas. The solid raw material is, for example, coal (such as lignite) or biomass (such as wood pellets). The gasification gas production apparatus 100 is a circulating fluidized bed gasification system. That is, the gasification gas production apparatus 100 circulates a fluidized medium as a heat medium through the combustion furnace 110, the second pipe 114, the cyclone 120, the third pipe 122, the gasification furnace 130, and the first pipe 112. The fluidized medium is silica sand with a particle size of approximately 300 μm.

[0019] The combustion furnace 110 has a cylindrical shape. A first pipe 112 connects the lower part of the combustion furnace 110 to the gasification furnace 130, which will be described later. Fuel and a bed material are introduced into the combustion furnace 110 from the gasification furnace 130 through the first pipe 112. In the combustion furnace 110, the fuel is combusted and the bed material is heated to a temperature of 900°C or higher and 1000°C or lower. A second pipe 114 connects the upper part of the combustion furnace 110 to the cyclone 120, which will be described later. The bed material and combustion exhaust gas heated in the combustion furnace 110 are sent to the cyclone 120 through the second pipe 114.

[0020] The cyclone 120 separates the mixture of the bed material and combustion exhaust gas introduced from the combustion furnace 110 through the second pipe 114 into solid and gas. The third pipe 122 connects the bottom of the cyclone 120 to the gasification furnace 130. The high-temperature bed material separated in the cyclone 120 is introduced into the gasification furnace 130 through the third pipe 122.

[0021] The high-temperature fluidized medium is fluidized by a fluidizing gas (e.g., steam) in the gasifier 130. Specifically, the gasifier 130 includes a storage vessel 132 and a steam inlet 134. The storage vessel 132 stores the fluidized medium and the solid raw material.

[0022] The water vapor introduction unit 134 introduces water vapor into the storage tank 132. The water vapor introduction unit 134 includes an air box 134a and a pump 134b. The air box 134a is provided below the storage tank 132. The top of the air box 134a also functions as the bottom of the storage tank 132. The top of the air box 134a is formed with a breathable dispersion plate. The pump 134b introduces water vapor into the air box 134a. The water vapor introduced into the air box 134a is introduced into the storage tank 132 from the bottom (dispersion plate) of the storage tank 132. The discharge side of the pump 134b is connected to the air box 134a. The pump 134b introduces water vapor into the air box 134a at a flow rate that allows a fluidized bed of the fluidized medium to be formed inside the storage tank 132. Therefore, the high-temperature fluidized medium introduced from the cyclone 120 is fluidized by the steam, and a fluidized bed (e.g., a bubbling fluidized bed) is formed in the storage tank 132. In addition, the pump 134b introduces steam in an amount of 0.5 mol to 2.0 mol relative to the carbon contained in the solid raw material stored in the storage tank 132.

[0023] Furthermore, as will be described in detail later, solid raw materials are introduced into the gasification furnace 130 (storage tank 132) from the dry distillation furnace 140. The introduced solid raw materials are gasified by the heat of the bed material, which is 700°C or more and 900°C or less, thereby producing gasified gas (synthesis gas). The gasified gas produced in the gasification furnace 130 is introduced into the refinery device 210 through a fourth pipe 136. The fourth pipe 136 connects the upper part of the gasification furnace 130 and the refinery device 210. The specific configuration of the refinery device 210 will be described in detail later.

[0024] Then, as described above, the fluidized bed material fluidized in the gasification furnace 130 is returned to the combustion furnace 110 through the first pipe 112 connecting the gasification furnace 130 and the combustion furnace 110 .

[0025] As described above, in the gasification gas production apparatus 100 according to this embodiment, the bed material moves through the combustion furnace 110, the second pipe 114, the cyclone 120, the third pipe 122, the gasification furnace 130, and the first pipe 112 in this order, and is then introduced back into the combustion furnace 110, thereby circulating through these.

[0026] The combustion exhaust gas separated by the cyclone 120 is heat exchanged (cooled) by a heat exchanger 124 (boiler). The combustion exhaust gas cooled by the heat exchanger 124 is denitrified by a denitration device 126. The combustion exhaust gas denitrified by the denitration device 126 is desulfurized by a desulfurization device 128. The combustion exhaust gas desulfurized by the desulfurization device 128 is exhausted to the outside.

[0027] Furthermore, the residue of the solid raw material is introduced into the combustion furnace 110 from the gasification furnace 130 through the first pipe 112. The residue of the solid raw material is used as fuel in the combustion furnace 110. The residue of the solid raw material is the portion of the solid raw material that remains without being gasified in the gasification furnace 130.

[0028] As described above, the gasification furnace 130 gasifies the solid raw material, but if the solid raw material is directly introduced into the gasification furnace 130, the tar content in the produced gasification gas will be high. Therefore, the gasification gas production apparatus 100 of this embodiment is equipped with a dry distillation furnace 140.

[0029] The carbonization furnace 140 carbonizes the solid feedstock using air. That is, the carbonization furnace 140 heats the solid feedstock to vaporize the tar and separate the tar from the solid feedstock. Specifically, the carbonization furnace 140 includes a main body 142 and an air inlet 144. The main body 142 is cylindrical. The main body 142 temporarily accommodates the solid feedstock. The solid feedstock is introduced into the main body 142 from its upper portion. A fifth pipe 150 connects the lower portion of the carbonization furnace 140 to the third pipe 122. The solid feedstock is introduced from the main body 142 to the gasification furnace 130 through the fifth pipe 150 and the third pipe 122. That is, the solid feedstock moves from top to bottom within the main body 142.

[0030] The air introduction part 144 is, for example, a pump. The discharge side of the air introduction part 144 is connected to the lower part of the main body 142. The air introduction part 144 introduces air (for example, air at room temperature (25°C)) into the main body 142. The air introduced into the main body 142 by the air introduction part 144 moves vertically upward. Therefore, the air flows opposite to the solid raw material.

[0031] When the solid feedstock comes into contact with air within the main body 142, volatile components (tar, hydrogen, hydrocarbons, etc.) contained in the solid feedstock are partially oxidized by oxygen in the air. The heat of reaction generated by the partial oxidation heats the solid feedstock. In this embodiment, the air inlet 144 introduces air so that the temperature inside the main body 142 (the temperature of the solid feedstock) falls within a predetermined carbonization temperature range. The lower limit of the carbonization temperature range is a temperature (e.g., 250°C) at which tar does not condense. The upper limit of the carbonization temperature range is a temperature (e.g., 550°C) below the temperature at which tar separated (vaporized) from the solid feedstock is completely combusted (oxidized).

[0032] In this way, the carbonization furnace 140 heats the solid feedstock to within the carbonization temperature range, thereby carbonizing the solid feedstock. In other words, the carbonization furnace 140 vaporizes and separates tar from the solid feedstock. In this way, the solid feedstock from which the tar has been separated (removed) (solid feedstock in which 90% or more of the combustible content is carbon) is introduced by its own weight into the gasification furnace 130 through the fifth piping 150 and the third piping 122. As a result, almost no tar is introduced into the gasification furnace 130, making it possible to reduce the tar content in the gasification gas produced in the gasification furnace 130. Furthermore, since the carbonization furnace 140 heats the solid feedstock to within the carbonization temperature range, it is possible to remove water from the solid feedstock.

[0033] Meanwhile, the tar separated (vaporized) in the carbonization furnace 140 flows upward as a carbonization gas within the carbonization furnace 140. The carbonization gas is then introduced into the combustion furnace 110 through a sixth pipe 152 connected to the upper part of the carbonization furnace 140. The sixth pipe 152 connects the upper part of the carbonization furnace 140 with the lower part of the combustion furnace 110. The combustion furnace 110 burns the carbonization gas as fuel to heat a fluidized medium. This makes it possible to convert the carbonization gas into thermal energy in the combustion furnace 110. Furthermore, it becomes possible to thermally decompose the carbonization gas (tar) in the combustion furnace 110.

[0034] In addition to tar, the dry distillation gas contains hydrocarbons, hydrogen, nitrogen components (ammonia (NH3), hydrogen cyanide (HCN), etc.), and sulfur components (hydrogen sulfide (HS), carbonyl sulfide (COS), carbon disulfide (CS2), etc.). The hydrocarbons and hydrogen contained in the dry distillation gas are used as fuel in the combustion furnace 110, just like the tar. The nitrogen components contained in the dry distillation gas are removed by the denitration device 126. The sulfur components contained in the dry distillation gas are removed by the desulfurization device 128.

[0035] Fig. 2 is a diagram illustrating the refining device 210. In Fig. 2, the flow of gasification gas is indicated by solid arrows, and the flow of wastewater is indicated by dashed arrows.

[0036] The purification device 210 purifies the gasification gas produced by the gasification furnace 130. Specifically, the purification device 210 includes a heat exchanger 212, a direct cooler 214, a mist eliminator 216, a pressure booster 218, and a wastewater treatment device 220.

[0037] The heat exchanger 212 exchanges heat between the gasification gas produced by the gasification furnace 130 and steam. The heat exchanger 212 recovers the sensible heat of the gasification gas with steam, and sets the outlet temperature of the gasification gas to about 200°C. As described above, the gasification gas production apparatus 100 is equipped with the dry distillation furnace 140, and therefore the gasification gas produced by the gasification furnace 130 contains almost no tar. Therefore, the gasification gas can be cooled in the heat exchanger 212 to a temperature below the temperature (250°C) at which tar condenses. In other words, it is possible to improve the heat recovery efficiency of the heat exchanger 212.

[0038] The direct cooler 214 is composed of, for example, a spray tower. The direct cooler 214 scrubs the gasified gas with water. Specifically, the direct cooler 214 cools the gasified gas at about 200°C to about 70°C by spraying water at about 40°C onto the gasified gas. In this way, the direct cooler 214 condenses sludge remaining in the gasified gas and removes it from the gasified gas. The mist eliminator 216 is composed of, for example, a mist separator. The mist eliminator 216 scrubs the gasified gas with water. Specifically, the mist eliminator 216 sprays water droplets (at about 40°C) smaller in diameter than the cooling water sprayed by the direct cooler 214 onto the gasified gas. In this way, the mist eliminator 216 condenses sludge that could not be removed by the direct cooler 214 and removes it from the gasified gas.

[0039] As described above, the gasification gas production apparatus 100 includes the dry distillation furnace 140, and therefore the gasification gas produced by the gasification furnace 130 contains almost no tar. This eliminates the need to condense tar in the direct cooler 214 and the mist eliminator 216, allowing for a reduction in the amount of water sprayed onto the gasification gas. This makes it possible to reduce the size of the direct cooler 214 and the mist eliminator 216. Furthermore, it is possible to reduce the amount of wastewater discharged from the direct cooler 214 and the mist eliminator 216 to the wastewater treatment device 220, which will be described later.

[0040] The booster 218 is configured by, for example, a blower, a compressor, a turbo pump, or a positive displacement pump. The booster 218 boosts the pressure of the gasification gas cooled by the mist eliminator 216 to 0.1 MPa to 5 MPa. The gasification gas thus purified (purified gasification gas) is sent to downstream equipment.

[0041] The wastewater treatment unit 220 removes sludge from the wastewater produced in the direct cooler 214, the mist eliminator 216, and the booster 218.

[0042] [Gasification gas production method] Next, a method for producing gasification gas using the gasification gas producing apparatus 100 will be described. Fig. 3 is a flowchart illustrating the process flow of the method for producing gasification gas. As shown in Fig. 3, the method for producing gasification gas includes a dry distillation step S110, a gasification step S120, and a purification step S130. Each step will be described in detail below.

[0043] [Carry distillation process S110] The dry distillation step S110 is a step in which the dry distillation furnace 140 dry distills the solid raw material with air.

[0044] [Gasification process S120] The gasification step S120 is a step in which the gasification furnace 130 gasifies the solid raw material dry-distilled in the dry-distillation step S110 using the heat of the bed material.

[0045] [Purification step S130] The refining step S130 is a step in which the refining device 210 purifies the gasification gas produced in the gasification step S120.

[0046] As described above, the gasification gas production apparatus 100 of this embodiment is equipped with the carbonization furnace 140. Furthermore, the method for producing gasification gas using the gasification gas production apparatus 100 carbonizes a solid raw material. As a result, the gasification gas production apparatus 100 and the method for producing gasification gas using the same can reduce the tar content in the gasification gas produced in the gasification furnace 130. Therefore, the purification apparatus 210 can omit the oxidation reforming furnace, deammoniation device, and desulfurization device.

[0047] That is, the gasification gas producing apparatus 100 of the present embodiment generates less wastewater than the conventional wet method. Therefore, the gasification gas producing apparatus 100 can reduce the cost required for treating wastewater compared to the conventional wet method.

[0048] Furthermore, unlike the conventional dry process, the gasification gas production apparatus 100 of this embodiment can omit the oxidation reforming furnace. Therefore, the gasification gas production apparatus 100 can improve cold gas efficiency compared to the conventional dry process.

[0049] In other words, the gasification gas production apparatus 100 and the method for producing gasification gas using the same can remove tar from the gasification gas more efficiently than conventional wet and dry methods.

[0050] [Variations] Fig. 4 is a diagram illustrating a modified gasification gas production apparatus 300. As shown in Fig. 4, the gasification gas production apparatus 300 includes a combustion furnace 110, a first pipe 112, a second pipe 114, a cyclone 120, a third pipe 122, a gasification furnace 130, a fourth pipe 136, a dry distillation furnace 140, a fifth pipe 150, a purification device 210, a cooling section 310, a seventh pipe 312, a junction pipe 314, and a separator 320. Note that components that are substantially the same as those in the gasification gas production apparatus 100 are denoted by the same reference numerals, and description thereof will be omitted.

[0051] The cooling section 310 is configured, for example, by a spray tower. The seventh pipe 312 connects the upper part of the main body 142 of the carbonization furnace 140 to the cooling section 310. The cooling section 310 cools the carbonization gas discharged from the carbonization furnace 140 through the seventh pipe 312 to a temperature at which the tar condenses. The configuration including the cooling section 310 condenses (liquefies) the tar in the carbonization gas. This makes it possible to remove the tar from the carbonization gas. In other words, the cooling section 310 produces a purified carbonization gas containing hydrocarbons and hydrogen.

[0052] The junction pipe 314 is a pipe that connects the cooling section 310 and the fourth pipe 136. That is, the purified dry distillation gas generated by the cooling section 310 is sent to the purification device 210 (heat exchanger 212) through the junction pipe 314 together with the gasification gas produced in the gasification furnace 130.

[0053] The separator 320 separates the wastewater generated in the cooling section 310 into light tar, heavy tar, and treated water. The light tar and heavy tar separated by the separator 320 are combusted in the combustion furnace 110 or sold as a product. The treated water separated by the separator 320 is introduced into the combustion furnace 110. This allows the combustion furnace 110 to combust water-soluble tar contained in the treated water.

[0054] As described above, the gasification gas production apparatus 300 of the modified example is configured to include the cooling section 310 and the junction pipe 314, thereby making it possible to increase the amount of combustible gas sent to the refinement apparatus 210. In other words, the gasification gas production apparatus 300 can increase the amount of refined gasification gas that becomes a product.

[0055] [Example] Thermogravimetric-differential thermal analysis (TG-DTA) of lignite was performed under a nitrogen atmosphere. Figure 5 shows the results of the thermogravimetric-differential thermal analysis of lignite. In Figure 5, the vertical axis represents the weight loss rate (mg / sec) of the lignite, and the horizontal axis represents the atmospheric temperature (°C).

[0056] As shown in Figure 5, the weight loss rate of lignite increased when the ambient temperature reached approximately 100°C. This was due to the evaporation of water from the lignite. Furthermore, the weight loss rate of lignite increased when the ambient temperature reached 250°C or higher, and reached its highest rate (-0.010 mg / sec) when the ambient temperature reached approximately 430°C. Furthermore, as the ambient temperature increased from 430°C, the weight loss rate of lignite gradually decreased, and when the ambient temperature exceeded 550°C, the weight loss rate of lignite was -0.004 mg / sec.

[0057] From the above analysis results, it was confirmed that when lignite is heated to between 250°C and 550°C, the volatile components contained in the lignite (tar, hydrogen, hydrocarbons, etc.) vaporize.

[0058] Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the above-described embodiments. It is clear that a person skilled in the art can conceive of various modifications or alterations within the scope of the claims, and it is understood that these also naturally fall within the technical scope of the present disclosure.

[0059] For example, in the above-described embodiment and modified examples, the dry distillation furnace 140 has been described as being configured to dry distill the solid raw material using air. However, the dry distillation furnace 140 may dry distill the solid raw material using an oxygen-containing gas other than air. By introducing a gas containing at least oxygen (oxygen-containing gas) into the main body 142, volatile components contained in the solid raw material can be partially oxidized. In other words, by simply bringing the oxygen-containing gas into contact with the solid raw material, the solid raw material can be heated and dry distilled without the need for a separate heating device.

[0060] Furthermore, the carbonization furnace 140 may carbonize the solid raw material using combustion exhaust gas instead of or in addition to the oxygen-containing gas. This allows the solid raw material to be heated by the heat of the combustion exhaust gas. In other words, the solid raw material can be carbonized by simply bringing the combustion exhaust gas into contact with the solid raw material, without the need for a separate heating device. The combustion exhaust gas may be combustion exhaust gas separated by the cyclone 120, or may be combustion exhaust gas discharged from other equipment (such as a boiler).

[0061] In the above embodiment and modified examples, the gasifier 130 has been described as being configured to gasify the solid raw material in a fluidized bed of a fluidized medium. However, the gasifier 130 may be configured to gasify the solid raw material using the heat of the fluidized medium. The gasifier 130 may also gasify the solid raw material in a moving bed of a fluidized medium, for example.

[0062] Furthermore, in the above embodiment and modified examples, the gasification furnace 130 has been described as having a configuration including the steam introduction unit 134. However, the gasification furnace 130 does not have to have the steam introduction unit 134. In other words, the gasification furnace 130 may gasify the solid raw material using a gasifying agent other than steam. For example, the gasification furnace 130 may gasify the solid raw material using carbon dioxide.

[0063] In the above modification, an example has been described in which all of the pyrolysis gas cooled by the cooling section 310 is merged into the fourth pipe 136. However, a portion of the pyrolysis gas cooled by the cooling section 310 may be introduced into the combustion furnace 110.

[0064] Furthermore, in the above modification, the junction pipe 314 is connected to the fourth pipe 136. However, the junction pipe 314 may be directly connected to the refinery device 210 (heat exchanger 212). [Industrial Applicability]

[0065] The present disclosure can be used in a gasification gas production apparatus and a gasification gas production method. [Explanation of symbols]

[0066] 100 Gasification gas production equipment 110 Combustion furnace 130 Gasifier 132 Containment Tank 134 Steam inlet 140 Dry distillation furnace 142 Main Unit 144 Air intake section 300 Gasification gas production equipment 310 Cooling section

Claims

1. a carbonization furnace having a main body that accommodates a solid raw material and a gas inlet that introduces an oxygen-containing gas into the main body, wherein the solid raw material is carbonized by heating the solid raw material to a temperature of 250°C or higher and 550°C or lower using reaction heat generated by partially oxidizing a volatile component contained in the solid raw material with oxygen in the oxygen-containing gas; a gasification furnace having a storage tank that stores the dry-distilled solid material and a fluidized medium, and a steam inlet that introduces steam into the storage tank, and gasifies the dry-distilled solid material using heat possessed by the fluidized medium; Equipped with The gasification gas production apparatus is configured such that a mixture obtained by mixing the dry-distilled solid raw material and the bed material is introduced into the storage tank of the gasification furnace.

2. The solid raw material is introduced into the body of the dry distillation furnace from an upper portion of the body, The mixture obtained by mixing the solid raw material discharged from the lower part of the main body of the dry distillation furnace with the bed material is introduced into the storage tank of the gasification furnace, The gas inlet of the dry distillation furnace introduces the oxygen-containing gas from a lower part of the main body, The gasification gas producing apparatus according to claim 1 , wherein the carbonization gas is discharged from an upper portion of the main body of the carbonization furnace.

3. a combustion furnace that burns the carbonization gas discharged from the carbonization furnace to heat a fluidized medium; 3. The gasification gas production apparatus according to claim 1, wherein a bed material heated by the combustion furnace is introduced into the gasification furnace.

4. a cooling unit that cools the dry distillation gas discharged from the dry distillation furnace to a temperature at which tar condenses, 4. The gasification gas production apparatus according to claim 1, wherein the gas cooled by the cooling section is delivered together with the gasification gas produced in the gasification furnace.

5. 5. The gasification gas producing apparatus according to claim 1, wherein the steam introducing section introduces the steam at a flow rate capable of forming a fluidized bed of the fluidized medium in the storage vessel.

6. In a dry distillation furnace having a body for accommodating a solid raw material, the solid raw material is heated to 250°C or higher and 550°C or lower by reaction heat generated by partially oxidizing a volatile component contained in the solid raw material with oxygen in an oxygen-containing gas, thereby dry distilling the solid raw material; The mixture obtained by mixing the dry-distilled solid raw material with the fluidized medium is introduced into a gasification furnace; The method for producing a gasification gas includes gasifying the dry-distilled solid raw material with the heat of the bed material in the gasification furnace using steam as a gasifying agent.

7. The solid raw material is introduced into the body of the dry distillation furnace from an upper portion of the body, The mixture obtained by mixing the solid raw material discharged from the lower part of the main body of the dry distillation furnace with the bed material is introduced into the gasification furnace, the oxygen-containing gas is introduced from the lower part of the body of the carbonization furnace; The method for producing gasification gas according to claim 6, wherein the carbonization gas is discharged from an upper portion of the main body of the carbonization furnace.

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