JP7727366B2 - Gasification gas production apparatus and gasification gas production method - Google Patents

Description

This disclosure relates to a gasification gas production apparatus and a method for producing gasification gas.

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. With technology that gasifies solid feedstocks at these low temperatures, the tar contained in the solid feedstock is contained in large quantities in the resulting gasified gas. Tar condenses when cooled to below 250°C. As a result, tar adheres to and accumulates on equipment and piping downstream of the gasification furnace. This can lead to problems such as clogged piping and poisoning of catalysts contained in the equipment.

Wet and dry methods have been proposed as technologies for removing tar from gasification gas. The wet method involves spraying water onto the gasification gas to cool it, condensing the tar, and then separating and removing it (see, for example, Patent Document 1). The dry method involves partially oxidizing (burning) part of the gasification gas, raising the temperature to around 1,300°C, and decomposing and removing the tar (see, for example, Patent Document 2).

Patent No. 5217292 Patent No. 5217295

The above-mentioned wet method generates large amounts of wastewater containing tar, resulting in high wastewater treatment costs. Furthermore, the above-mentioned dry method 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 feedstock) compared to the wet method. Therefore, there is a need to develop technology that can reduce the tar content in the gasification gas produced in a gasification furnace.

In light of these issues, the present disclosure aims to provide a gasification gas production apparatus and a method for producing gasification gas that can reduce the tar content in the gasification gas produced in a gasification furnace.

In order to solve the above problems, a gasification gas production apparatus according to one embodiment of the present disclosure comprises: a carbonization furnace having a main body for accommodating a solid raw material; and a gas inlet section for introducing an oxygen-containing gas into the main body, wherein the solid raw material is heated to 250°C or higher and 550°C or lower by reaction heat generated by partial oxidation of volatile components contained in the solid raw material by oxygen in the oxygen-containing gas, thereby carbonizing the solid raw material; and a gasification furnace having a storage tank for accommodating the carbonized solid raw material and a fluidized medium, and a steam inlet section for introducing steam into the storage tank, wherein the carbonized solid raw material is gasified by the heat possessed by 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.

The gasification furnace may also be equipped with a combustion furnace that burns the carbonization gas discharged from the carbonization furnace to heat the bed material, and the bed material heated by the combustion furnace may be introduced into the gasification furnace.

The system may also be equipped with a cooling unit that cools the dry distillation gas discharged from the dry distillation furnace to a temperature at which tar condenses, and the gas cooled by the cooling unit may be discharged together with the gasification gas produced in the gasification furnace.

The water vapor introduction section may also introduce water vapor at a flow rate that allows a fluidized layer of the fluidized medium to form within the storage tank.

In order to solve the above problems, a method for producing a gasification gas according to one embodiment of the present disclosure comprises the steps of: in a dry distillation furnace having a main body for accommodating a solid raw material, using the reaction heat generated by partially oxidizing volatile components contained in the solid raw material with oxygen in an oxygen- containing gas, heating the solid raw material to 250°C or higher and 550°C or lower to dry distill the solid raw material; mixing the dry distilled solid raw material with a fluidized medium, and introducing the resulting mixture into a gasification furnace; and in the gasification furnace, using steam as a gasifying agent, gasifying the dry distilled solid raw material with the heat possessed by the fluidized medium.
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.

This disclosure makes it possible to reduce the tar content in the gasification gas produced in a gasification furnace.

FIG. 1 is a diagram illustrating a gasification gas production apparatus. FIG. 2 is a diagram illustrating a refining device. 1 is a flowchart illustrating a process flow of a method for producing gasification gas. FIG. 10 is a diagram illustrating a modified example of a gasification gas production apparatus. FIG. 1 is a diagram showing the results of thermogravimetric differential thermal analysis of lignite.

Embodiments of the present disclosure will be described in detail below with reference to the accompanying drawings. Dimensions, materials, and other specific values shown in these embodiments are merely examples for ease of understanding and, unless otherwise specified, do not limit the present disclosure. Furthermore, 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.

Figure 1 is a diagram illustrating a gasification gas production system 100. As shown in Figure 1, the gasification gas production system 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. Note that in Figure 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.

The gasification gas production system 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 system 100 is a circulating fluidized bed gasification system. In other words, the gasification gas production system 100 circulates a fluidized medium as a heat medium through the combustion furnace 110, second pipe 114, cyclone 120, third pipe 122, gasification furnace 130, and first pipe 112. The fluidized medium is silica sand with a particle size of approximately 300 μm.

The combustion furnace 110 is cylindrical. The first pipe 112 connects the lower part of the combustion furnace 110 to the gasification furnace 130, which will be described later. Fuel and 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. The 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.

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.

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 tank 132 and a steam inlet 134. The storage tank 132 stores the fluidized medium and solid raw material.

The water vapor introduction section 134 introduces water vapor into the storage tank 132. The water vapor introduction section 134 includes a wind box 134a and a pump 134b. The wind box 134a is provided below the storage tank 132. The top of the wind box 134a also functions as the bottom of the storage tank 132. The top of the wind box 134a is composed of a breathable dispersion plate. The pump 134b introduces water vapor into the wind box 134a. The water vapor introduced into the wind 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 wind box 134a. The pump 134b introduces water vapor into the wind box 134a at a flow rate that can form a fluidized layer of bed material within the storage tank 132. Therefore, the high-temperature fluidized medium introduced from cyclone 120 is fluidized by the steam, forming a fluidized bed (e.g., a bubbling fluidized bed) within storage tank 132. Furthermore, pump 134b introduces steam in an amount of 0.5 moles to 2.0 moles relative to the carbon contained in the solid raw material stored in storage tank 132.

As will be described in more detail below, 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 between 700°C and 900°C, thereby producing gasified gas (synthesis gas). The gasified gas produced in the gasification furnace 130 is introduced into the refinery device 210 through the fourth piping 136. The fourth piping 136 connects the upper part of the gasification furnace 130 to the refinery device 210. The specific configuration of the refinery device 210 will be described in more detail below.

Then, as described above, the fluidized bed material 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.

In this way, in the gasification gas production apparatus 100 according to this embodiment, the bed material moves through the combustion furnace 110, the second piping 114, the cyclone 120, the third piping 122, the gasification furnace 130, and the first piping 112 in that order, before being introduced back into the combustion furnace 110, thereby circulating through these components.

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

In addition, the solid raw material residue is introduced into the combustion furnace 110 from the gasification furnace 130 via the first pipe 112. The solid raw material residue is used as fuel in the combustion furnace 110. The solid raw material residue is the solid raw material that remains ungasified in the gasification furnace 130.

As explained above, the gasification furnace 130 gasifies solid raw materials, but if the solid raw materials are introduced directly 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.

The carbonization furnace 140 carbonizes the solid feedstock using air. That is, the carbonization furnace 140 heats the solid feedstock, vaporizes the tar, and separates 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 stores the solid feedstock. The solid feedstock is introduced into the main body 142 from its upper portion. The 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 via the fifth pipe 150 and the third pipe 122. That is, the solid feedstock moves from top to bottom within the main body 142.

The air introduction section 144 is, for example, a pump. The discharge side of the air introduction section 144 is connected to the bottom of the main body 142. The air introduction section 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 section 144 moves vertically upward. Therefore, the air flows opposite the solid raw material.

When the solid feedstock comes into contact with air within the main body 142, the volatile components contained in the solid feedstock (tar, hydrogen, hydrocarbons, etc.) are partially oxidized by oxygen in the air. The heat of reaction generated by the partial oxidation then 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).

In this way, the carbonization furnace 140 carbonizes the solid feedstock by heating it to within the carbonization temperature range. In other words, the carbonization furnace 140 vaporizes and separates the 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 pipe 150 and the third pipe 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, because the carbonization furnace 140 heats the solid feedstock to within the carbonization temperature range, it is possible to remove water from the solid feedstock.

Meanwhile, the tar separated (vaporized) in the carbonization furnace 140 flows upward within the carbonization furnace 140 as carbonization gas. The carbonization gas is then introduced into the combustion furnace 110 through a sixth pipe 152 connected to the top of the carbonization furnace 140. The sixth pipe 152 connects the top of the carbonization furnace 140 with the bottom of the combustion furnace 110. The combustion furnace 110 burns the carbonization gas as fuel to heat a fluidized medium. This allows the carbonization gas to be converted into thermal energy in the combustion furnace 110. It also makes it possible to thermally decompose the carbonization gas (tar) in the combustion furnace 110.

In addition to tar, the dry distillation gas contains hydrocarbons, hydrogen, nitrogen components (ammonia (NH ₃ ), hydrogen cyanide (HCN), etc.), and sulfur components (hydrogen sulfide (H ₂ S), carbonyl sulfide (COS), carbon disulfide (CS ₂ ), 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.

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

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 booster 218, and a wastewater treatment device 220.

The heat exchanger 212 exchanges heat between the gasified gas produced by the gasification furnace 130 and steam. The heat exchanger 212 recovers the sensible heat of the gasified gas using steam, raising the outlet temperature of the gasified gas to approximately 200°C. As described above, the gasification gas production apparatus 100 is equipped with the dry distillation furnace 140, so the gasified gas produced by the gasification furnace 130 contains almost no tar. Therefore, the gasified gas can be cooled in the heat exchanger 212 to a temperature below the tar condensation temperature (250°C). In other words, the heat recovery efficiency of the heat exchanger 212 can be improved.

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

As described above, the gasification gas production apparatus 100 is equipped with the dry distillation furnace 140, so 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 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 mist eliminator 216. It also reduces the amount of wastewater discharged from the direct cooler 214 and mist eliminator 216 to the wastewater treatment unit 220, which will be described later.

The booster 218 is composed of, for example, a blower, compressor, turbo pump, or positive displacement pump. The booster 218 pressurizes the gasification gas cooled by the mist eliminator 216 to 0.1 MPa to 5 MPa. The purified gasification gas (purified gasification gas) is then sent to downstream equipment.

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

[Method of producing gasification gas]
Next, a method for producing gasification gas using the gasification gas production 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.

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

[Gasification step 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.

[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.

As described above, the gasification gas production apparatus 100 of this embodiment is equipped with a dry distillation furnace 140. Furthermore, the method for producing gasification gas using the gasification gas production apparatus 100 dry distills a solid feedstock. As a result, the gasification gas production apparatus 100 and the method for producing gasification gas using it can reduce the tar content in the gasification gas produced in the gasification furnace 130. Therefore, the refining apparatus 210 can omit the oxidation reforming furnace, deammoniation device, and desulfurization device.

In other words, the gasification gas production apparatus 100 of this embodiment generates less wastewater than conventional wet processes. Therefore, the gasification gas production apparatus 100 can reduce the cost required for wastewater treatment compared to conventional wet processes.

Furthermore, unlike conventional dry processes, 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 conventional dry processes.

In other words, the gasification gas production apparatus 100 and the gasification gas production method using it can more efficiently remove tar from gasification gas than conventional wet and dry methods.

[Modification]
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.

The cooling section 310 is configured, for example, as 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 allows the tar to be removed from the carbonization gas. In other words, the cooling section 310 produces a purified carbonization gas containing hydrocarbons and hydrogen.

The junction pipe 314 is a pipe that connects the cooling section 310 and the fourth pipe 136. In other words, the purified dry distillation gas produced by the cooling section 310 is sent to the purification device 210 (heat exchanger 212) via the junction pipe 314, together with the gasification gas produced in the gasification furnace 130.

The separator 320 separates the wastewater produced 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 the water-soluble tar contained in the treated water.

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

[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).

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 reached -0.004 mg/sec.

These analysis results confirm that when lignite is heated to temperatures between 250°C and 550°C, the volatile components contained in the lignite (tar, hydrogen, hydrocarbons, etc.) vaporize.

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 could conceive of various modifications or alterations within the scope of the claims, and it is understood that these naturally fall within the technical scope of the present disclosure.

For example, in the above-described embodiment and modified examples, the dry distillation furnace 140 was described as being configured to dry distill the solid raw material using air. However, the dry distillation furnace 140 may also 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, it is possible to partially oxidize the volatile components contained in the solid raw material. 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.

The dry distillation furnace 140 may also dry distill 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 using the heat contained in the combustion exhaust gas. In other words, by simply bringing the combustion exhaust gas into contact with the solid raw material, the solid raw material can be dry distilled without the need for a separate heating device. The combustion exhaust gas may be combustion exhaust gas separated by the cyclone 120, or combustion exhaust gas discharged from other equipment (such as a boiler).

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

Furthermore, in the above embodiment and modified examples, a configuration in which the gasifier 130 includes a steam introduction section 134 has been described as an example. However, the gasifier 130 does not have to include a steam introduction section 134. In other words, the gasifier 130 may gasify the solid raw material using a gasifying agent other than steam. For example, the gasifier 130 may gasify the solid raw material using carbon dioxide.

Furthermore, in the above modified example, an example was given of a configuration in which all of the dry distillation gas cooled by the cooling section 310 is merged into the fourth pipe 136. However, a portion of the dry distillation gas cooled by the cooling section 310 may also be introduced into the combustion furnace 110.

Furthermore, in the above modified example, the junction pipe 314 is connected to the fourth pipe 136. However, the junction pipe 314 may also be connected directly to the purification device 210 (heat exchanger 212).

This disclosure can be used in gasification gas production equipment and gasification gas production methods.

100 Gasification gas production apparatus 110 Combustion furnace 130 Gasification furnace 132 Storage tank 134 Steam introduction section 140 Dry distillation furnace 142 Main body 144 Air introduction section 300 Gasification gas production apparatus 310 Cooling section

Claims (7)

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. The solid raw material is introduced into the main body of the carbonization furnace from an upper portion of the main 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. 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. 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. 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. In a dry distillation furnace having a main body for accommodating a solid raw material, the solid raw material is heated to 250°C or more and 550°C or less 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. The solid raw material is introduced into the main body of the carbonization furnace from an upper portion of the main 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.