JP2022030460A - Hydrogen production device - Google Patents

Abstract

To provide a hydrogen production device which, in a fluidized bed gasifier, solves a problem that partial combustion of a raw material causes graphitization of carbon on a surface of the raw material on which a film is thereby formed, resulting in no progression of its gasification and a problem that half of chemical energy of the carbon as the raw material is changed into heat, resulting in low efficiency of conversion into hydrogen.SOLUTION: A raw material G including carbon is heat-decomposed and the resultant is divided into a solid portion and a volatile portion. Then, the solid portion is gasified in a bubbling fluidized bed 8 with a fuel cell 6 installed therein while the volatile portion is drawn above the fluidized bed and is gasified, improving efficiency of conversion of the carbon. Produced gas including carbon monoxide is converted into hydrogen gas in a shift reactor 23. Heat generated by electric power generation of the fuel cell is used to gasify the raw material and there is no combustion process, thereby enabling provision of a high efficiency hydrogen production device.SELECTED DRAWING: Figure 1

Description

The present invention relates to an apparatus for producing hydrogen gas by a thermochemical method, and more particularly to an apparatus for producing hydrogen gas from raw materials using a fluidized bed.

Hydrogen is not only an important industrial gas used in the chemical industry and petroleum refining, but in recent years, hydrogen energy is expected to play an important role as clean energy that does not generate environmentally hazardous substances. Therefore, the development of hydrogen production technology is being widely promoted. The method for producing hydrogen is roughly classified into an electrochemical method and a thermochemical method.

As an electrochemical method, there is a method of producing hydrogen by electrolysis of water using electric energy. Above all, the method of producing hydrogen using electric power obtained from natural energy such as solar power generation, wind power generation and hydroelectric power generation is said to have a small environmental load because it does not generate carbon dioxide.

Thermochemical methods include steam reforming, partial oxidation, and self-thermal reforming. The steam reforming method is a method of obtaining synthetic gas by reacting fossil fuels such as natural gas and naphtha with steam in an environment where a high temperature and a catalyst are present. For example, a technique of gasifying fossil fuels such as coal with a fluidized bed to generate hydrogen gas by a shift reaction is widely known. Further, a method of spraying steam on red-hot coke to obtain a mixed gas of carbon monoxide and hydrogen gas is known.

Patent Document 1 describes, as thermochemical methods, a fluidized layer gas furnace for gasifying raw materials containing carbon, a fuel cell installed in the fluidized layer gas furnace, and a generated gas gasified in the fluidized layer gas furnace. Disclosed is a gasification facility having a shift reactor that produces hydrogen from a fuel cell and using hydrogen gas generated by the shift reactor to generate electricity in a fuel cell.

Further, in Patent Document 2, the gasified gas generated in the coal gasification furnace is reformed into hydrogen gas in the shift reactor and supplied to the fuel cell to generate electricity, and is supplied to the gas turbine to generate electricity. The technology is disclosed.

International Publication No. 2013/005699 Japanese Unexamined Patent Publication No. 2008-291081 Tokusho No. 5-87757 Gazette

The present invention relates to an apparatus that uses a fluidized bed gasification furnace to bring raw materials such as organic compounds, biomass, and coal into contact with steam to convert them into carbon dioxide and hydrogen. A fluidized bed gasifier using an internal circulation type fluidized bed furnace having a two-chamber fluidized bed in which a partition member is provided in the fluidized bed so that the fluidized material in the heat recovery chamber is returned to the combustion chamber is known. (For example, Patent Document 3).

In many known fluidized bed gasifiers, the heat required to gasify the fossil fuel as a raw material is obtained by burning a part of the raw material. A part of the hydrogen gas that should be taken out as a product is converted into heat by burning the raw material, and the amount of hydrogen gas generated is reduced. As a result, it cannot be said that the carbon content contained in the raw material is fully utilized.

Further, in many fluidized bed gasification furnaces, there is a problem that carbon on the surface of the raw material is graphitized by partial combustion of the raw material, and a film is formed on the surface of the raw material to hinder the progress of the gasification reaction.

In a fluidized bed gasifier, excessive heating of the raw material may result in burning of the raw material. When the raw material is heated rapidly, dehydration and decomposition cannot keep up with the temperature rise, volatile matter is removed immediately, and secondary carbonization or condensation does not occur, so the yield of carbonized material decreases, and tar etc. are replaced. Will be increased. Furthermore, if tar content adheres to the surface of the raw material, it will hinder the promotion of gasification.

An object of the present invention is to solve the above-mentioned problems, and to provide a hydrogen production apparatus capable of effectively utilizing resources by increasing the conversion rate of carbon contained in raw materials into hydrogen. To provide. Further, the present invention provides a hydrogen production apparatus having high energy conversion efficiency, which has a small heat loss regardless of partial combustion of raw materials for the heat required for gasification.

In order to achieve the above-mentioned object, the hydrogen production apparatus according to the present invention heats a raw material to generate a descending fluidized bed that separates into volatile components and solids, and heats the solids to generate a first produced gas. It has a bubbling fluidized bed, and has an internal circulation type fluidized bed in which the descending moving layer and the bubbling fluidized bed are separated by a partition member. In the hydrogen production apparatus according to the present invention, the solid content heating means is arranged in the bubbling fluidized bed.

The downflow moving bed and the bubbling fluidized bed may be collectively referred to as a fluidized bed. In this configuration, carbon, hydrocarbons, or a mixture of carbon and hydrocarbons, biomass, livestock manure, and the like can be considered as raw materials supplied to the descending moving layer. The raw material is a carbon source and a reducing agent. The raw material is preferably charged into the descending flow moving layer from a hopper or the like.

The hydrogen production apparatus according to the present invention aims to fluidize the bubbling fluidized bed by supplying water vapor to the bubbling fluidized bed. According to this configuration, there is a windbox at the bottom of the fluidized bed gasifier, and the steam required for fluidization of the fluidized bed is blown from the windbox into the bubbling fluidized bed.

In the hydrogen production apparatus according to the present invention, the heat required for gasifying the solid content is not based on the partial combustion of the solid content, but by the heating means. According to this configuration, the raw material is gasified without partial combustion, so that the efficiency of gasification is excellent.

In the hydrogen production apparatus according to the present invention, the heating means is a fuel cell. According to this configuration, since the fuel cell is installed in the bubbling fluidized bed, the heat generated by the fuel cell during the power generation reaction is directly transferred to the bubbling fluidized bed via the fluidized medium without waste, and the fluidized bed is effectively used. It supplies the heat required for gasification of solids in the gas furnace.

In the hydrogen production apparatus according to the present invention, the heating means is an electric heater. Further, in the hydrogen production apparatus according to the present invention, the heating means is a tube heat exchanger. These heating means also supply the heat required for gasification of the solid matter in the fluidized bed gas furnace.

In the hydrogen production apparatus according to the present invention, the water vapor can be supplied to the downward flow moving layer via the flow rate adjusting means. Further, in the hydrogen production apparatus according to the present invention, the flow rate adjusting means is adjusted according to the output of the temperature detecting means provided in the descending flow moving layer. According to this configuration, the amount of water vapor flowing in the downflow moving layer can be adjusted to prevent the carbon surface from becoming dense in the downflow moving layer and inhibiting the gasification reaction.

The hydrogen production apparatus according to the present invention does not supply air and oxygen to the bubbling fluidized bed. According to this configuration, water vapor is used as a gas for suspended suspension of the bubbling fluidized bed, and air is not used. If air is supplied to the bubbling fluidized bed, partial combustion of raw materials causes energy loss. Furthermore, nitrogen contained in the air is also heated, and energy loss occurs in this respect as well.

In the hydrogen production apparatus according to the present invention, the first produced gas and the second produced gas obtained by thermally decomposing the volatile matter are guided to the shift reactor to generate hydrogen gas. According to this configuration, carbon monoxide that may hinder the electrode reaction of the fuel cell can be removed.

In the hydrogen production apparatus according to the present invention, a tar decomposition apparatus for removing tar components contained in the first produced gas and the second produced gas is provided in front of the shift reactor.

In the hydrogen production apparatus according to the present invention, hydrogen from the shift reactor is supplied to the fuel cell and can be taken out of the system. Further, the hydrogen production apparatus according to the present invention supplies steam generated during power generation of the fuel cell to the bubbling fluidized bed.

In the hydrogen production apparatus according to the present invention, the heat required for gasification of the raw material and the solid content is not due to partial combustion of the raw material and the solid content.

In the hydrogen production apparatus according to the present invention, the first produced gas is generated by the heat generated by the partial combustion of the solid content by the oxygen gas supplied to the bubbling fluidized bed.

It has a descending fluidized bed that heats raw materials to separate them into volatile and solid components, and a bubbling fluidized bed that heats the solids to generate a first produced gas, and has the descending fluidized bed and the bubbling fluidized bed. Is an internal circulation type bubbling fluidized bed separated by a partition member, and a heating means may be arranged in the bubbling fluidized bed to form a hydrogen production apparatus.

In a general fluidized bed gasification furnace, air is blown from a wind box at the bottom of the furnace to fluidize a fluidized medium such as high-temperature sand in the layer with hot air, and the raw materials and the like are thermally decomposed in the fluidized bed. As a result, gasification is carried out. When air is sent into the fluidized bed with a blower or the like, the raw materials are burned by the oxygen contained in the air. If the combustion process is involved in power generation, an exergy loss occurs, which causes a decrease in the exergy ratio ΔG / ΔH. If air is used for fluidization, nitrogen will also be heated. However, in the fluidized bed gasification furnace in hydrogen production according to the present invention, steam generated by the power generation reaction of the fuel cell is used for fluidization. Since air is not taken in from the outside for fluidization, it is possible to prevent a decrease in the value of the exergy ratio ΔG / ΔH.

According to the present invention, the heat required for gasification is obtained without partial combustion of raw materials and solids. Therefore, by increasing the conversion rate of carbon contained in raw materials to hydrogen, effective use of resources can be achieved. It is possible to plan. Further, by preventing the rapid heating of the raw material, the promotion of gasification is not hindered.

Further, by utilizing the heat generated by the power generation from the fuel cell, hydrogen production with low heat loss and high energy efficiency is provided.

It is a basic block diagram of the hydrogen production apparatus which concerns on 1st Embodiment. It is a basic block diagram of the hydrogen production apparatus which concerns on 2nd Embodiment. It is a basic block diagram of the hydrogen production apparatus which concerns on 3rd Embodiment. It is a flow sheet of electric power-hydrogen co-production that co-produces electric power and hydrogen.

Hereinafter, embodiments according to the present invention will be described with reference to the drawings, but the present invention is not limited to these embodiments.

FIG. 1 is a diagram showing a basic configuration of a hydrogen production apparatus according to a first embodiment of the present invention. The fluidized bed gasifier 2 includes a window box 3 that serves as an intake for working gas, a bubbling fluidized bed 8 and a downward flow moving layer 7 located above the window box 3, and a bubbling fluidized bed 8 and a downward flow moving layer 7. The freeboard 10 located above is provided as a main component.

The wind box 3 and the bubbling fluidized bed 8 and the downward flow moving layer 7 are separated by a dispersion plate 4. The dispersion plate 4 is inclined from the downward flow moving layer 7 to the bubbling fluidized bed 8 and assists the movement of solids to the bubbling fluidized bed 8.

The bubbling fluidized bed 8 on the left side of FIG. 1 and the descending flow moving layer 7 on the right side are separated by a partition member 9. There is a lower opening 12 at the lower part of the partition member 9, and an upper space 13 at the upper part. The moving speed of the working medium in the bubbling fluidized bed 8 is made faster than the moving speed of the working medium in the descending flow moving layer 7, so that the fluid is circulated in the direction of the bold arrow in FIG.

Water vapor S is supplied from the lower part of the fluidized bed gasification furnace 2 to the fluidized bed gasifier 2 via the windbox 3, and the fluidized bed 5 is suspended and suspended in the bubbling fluidized bed 8. When air is used as the working fluid that suspends and suspends the fluid medium 5, the raw material is partially burned by oxygen in the air, and the nitrogen contained in the air is also heated, resulting in energy loss. The steam S serves as a source of water ( _H2O ) for producing hydrogen.

A fuel cell 6 is arranged in the bubbling fluidized bed 8. Here, the fuel cell 6 is preferably operated at a high temperature because it serves as a heat source for gasification. Specifically, a solid oxide fuel cell (SOFC) that requires an operating temperature of 800 to 1,000 ° C. is preferable.

The raw material G, which is a solid fuel, is charged into the descending flow moving layer 7 from the raw material charging unit 11 of the descending flow moving layer 7. The raw material G may be carbon, a hydrocarbon, an organic substance, or a mixture thereof. Although biomass is used in this embodiment, it may be a fossil fuel such as coal other than biomass. It may be methanol and ethanol, or it may be a polymer compound such as plastic. It may be cooking oil or heavy oil.

The downflow moving layer 7 forms a moving layer, and the raw material G supplied from the raw material input unit 11 descends in the downflow moving layer 7.

The raw material G is thermally decomposed by being heated by the heat from the bubbling fluidized bed 8 in the process of descending the descending flow moving layer 7, and is separated into a volatile content and a solid content. The volatile components include tar and hydrocarbons, which are sent out to the free board 10, undergoing thermal decomposition and reduced by steam to generate a second produced gas containing carbon monoxide and hydrogen gas as main components. The solid content contains carbon, which is fixed carbon, and is sent out to the bubbling fluidized bed 8 from the lower opening 12 provided at the lower part of the partition member 9.

In the bubbling fluidized bed 8, solid particles made of sand or the like having an appropriate size are arranged inside the fluidized bed 8 as a fluidized medium 5. Water vapor S is sent to the bubbling fluidized bed 8 via the windbox 3, and the fluidized medium 5 made of solid particles is suspended and suspended on the dispersion plate 4 to be fluidized. The flow medium 5 is a powder or granular material such as silica sand, alumina or iron particles, or a mixture thereof. Further, the flow medium 5 may be supported by a catalyst that reduces water to produce hydrogen. Examples of these catalysts include ash, sodium, potassium and calcium. Alumina may be supported on the flow medium 5. The fluidized medium 5 has a function of transferring heat to carbon in the bubbling fluidized bed 8.

The solid content sent from the descending flow moving layer 7 to the bubbling fluidized bed 8 contains carbon, a fluidized medium 5, ash, and the like, of which carbon is thermally decomposed in a temperature range of 900 ° C to 1000 ° C. Then, it is reduced with water to generate a first produced gas containing carbon dioxide and hydrogen as main components. The reaction in the bubbling fluidized bed 8 is shown in Eq. (1). This gasification reaction is reduction, and the heat (Q) required for the reaction is supplied from the fuel cell 6 installed in the fluid medium 5.
Q + C + 2H ₂ O → CO ₂ + 2H ₂ (1)

An electric heater may be used instead of the fuel cell 6 as a means for heating the solid content. Further, a heat exchanger of a type that guides the combustion gas of fossil fuel such as kerosene or gas into the tube may be used.

A heating means such as a fuel cell needs to be provided in the bubbling fluidized bed 8. This is because if these heating means are provided in the descending flow moving layer 7, the temperature of the descending flow moving layer 7 becomes high and "burning" occurs in the charged raw material, which leads to a reduction in the yield of hydrogen.

When tar is attached to the solid content during gasification in the bubbling fluidized bed 8, the gasification reaction is hindered. However, since the tar content is separated in the descending flow moving layer 7 and almost no tar content is attached to the solid content, the gasification reaction is not hindered by the tar content.

By making the supply amount of water vapor to the bubbling fluidized bed 8 larger than the supply amount of water vapor to the descending flow moving layer 7, the fluidized material of the bubbling fluidized bed 8 exceeds the partition member 9 and is transmitted from the upper space 13. It flows into the descending flow moving layer 7, and the fluid material of the descending flow moving layer 7 returns to the bubbling fluidized bed 8 from the lower part of the partition member 9. As a result, an internal circulation type fluidized bed composed of a bubbling fluidized bed 8 and a downward flow moving layer 7 is formed. That is, the circulation of the moving substance is maintained by making the moving speed of the substance in the bubbling fluidized bed 8 faster than that of the descending flow moving layer 7.

Carbon dioxide, water vapor, carbon monoxide, hydrogen, and dust are contained in the first generated gas generated from the solid content in the bubbling fluidized bed 8 and the second generated gas separated by the downflow moving layer 7 and thermally decomposed by the free board 10. These generated gases are contained and sent to the gas cleaning device 22 via the free board unit 10.

The produced gas sent to the gas cleaning device 22 (hereinafter, simply referred to as a produced gas unless otherwise specified) has a temperature of approximately 400 ° C. to 650 ° C. at the inlet of the gas cleaning device 22.
As the gas cleaning device 22, a cyclone type dust collector can be used, but a filter type dust collector may be adopted. The filter method is preferable because it has a high dust collecting property. In the temperature range of 400 ° C. to 650 ° C., a bag filter can be used as the gas cleaning device 22, but a cyclone may be used and a ceramic filter may be arranged further downstream thereof.

Solids such as ash and alkali metal salts removed by the gas cleaning device 22 are discharged to the outside of the system from a discharge channel (not shown). The generated gas from which ash and the like have been removed is sent to the shift reactor 23. A corrosive gas removing device (not shown) for removing corrosive gas such as hydrogen chloride and hydrogen sulfide contained in the produced gas may be provided between the gas cleaning device 22 and the shift reactor 23.

Inside the shift reactor 23, the pipe through which the generated gas flows is filled with a catalyst for increasing the reaction rate, for example, magnetite (Fe ₃ O ₄ ) or platinum. The high-temperature steam generated by the power generation reaction in the fuel cell 6 may be supplied to the shift reactor 23. Using the water content of the high-temperature steam, the shift reactor 23 reacts carbon monoxide in the produced gas with water to generate hydrogen gas. This reaction equation is shown in equation (2).
CO + H ₂ O → H ₂ + CO ₂ (2)

The generated gas processed by the shift reactor 23 passes through the IDF 24, carbon dioxide is separated and removed by the CO2 separation device 25 in the next stage, and carbon dioxide is discharged to the outside of the system. The hydrogen gas is sent to the hydrogen separation device 26 in the next stage.

In the hydrogen separation device 26, the hydrogen gas is separated from the water vapor and stored in the hydrogen tank 27. The hydrogen gas from the hydrogen separation device 26 is supplied to the anode (negative electrode) of the fuel cell 6 and can contribute to power generation.

Since the heat generated from the fuel cell 6 is substantially equal to the endothermic component of the gasification reaction, this heat can be used as a heat source for gasification in the bubbling fluidized bed 8. This enables gasification in the fluidized bed gasification furnace without partial combustion of carbon, so that energy-efficient power generation can be achieved.

When the temperature of the descending flow moving layer 7 becomes higher than a predetermined temperature, the carbon surface of the solid content is graphitized and inhibits the gasification reaction. Alternatively, the surface of the solid content becomes dense and inhibits the progress of gasification. The modified example of the first embodiment of the present invention corresponds to the above-mentioned problem, and is obtained by adding a new element described below to the first embodiment of the present invention.

The flow rate adjusting means 14 is arranged below the dispersion plate 4 and below the downward flow moving layer 7. A part of the water vapor S supplied from the wind box 3 can be supplied to the downward flow moving layer 7 via the flow rate adjusting means 14. That is, the amount of water vapor flowing in the downward flow moving layer 7 can be adjusted by the flow rate adjusting means 14 installed upstream of the dispersion plate 4.

The downflow moving layer 7 is provided with a temperature detector (not shown), and when the temperature of the downflow moving layer 7 exceeds a predetermined temperature, the flow rate adjusting device (not shown) operates the flow rate adjusting means 14. Then, the amount of water vapor S flowing into the downward flow moving layer 7 is increased. When the amount of water vapor S flowing into the downflow moving layer 7 increases, the temperature of the downflow moving layer 7 decreases. The amount of water vapor may be adjusted using an automatic control device or manually. The temperature detector may be a thermocouple, a resistance temperature detector, or a non-contact thermometer.

FIG. 2 shows the configuration of the hydrogen production apparatus according to the second embodiment of the present invention. The configuration example of FIG. 2 is a configuration in which a tar decomposition device 21 is added to the configuration of FIG. 1, and differences from the first embodiment will be described.

The pyrolysis gas containing the volatile matter separated by the downflow moving layer 7 contains a tar content containing a hydrocarbon as a main component. The tar content not only adversely affects the operation of the fuel cell 6, but may also damage the fuel cell 6. Further, if tar is attached to carbon or hydrocarbon, there is a problem that the shift reaction is difficult to proceed. Therefore, it is desirable to install the tar decomposition device 21 in front of the shift reactor 23.

In the pyrolysis apparatus 21, the pyrolysis gas and the first generated gas are circulated in the honeycomb passage carrying the high-temperature nickel-based or cobalt-based catalyst, so that the pyrolysis impurities such as tar and aromatic hydrocarbons are produced. Organochlorine compounds such as unsaturated hydrocarbons and dioxins are removed by thermal decomposition and sent to the gas cleaning device 22 in the next stage.

Since the process after the gas cleaning device 22 is the same as that of the first embodiment, the description thereof will be omitted.

FIG. 3 shows the configuration of the hydrogen production apparatus according to the third embodiment of the present invention. What is characteristic of the configuration example of FIG. 3 is that the fuel cell installed in the bubbling fluidized bed is omitted in the configuration of the first embodiment. Hereinafter, the differences from the first embodiment will be mainly described.

As a means for heating the solid content, heat from partial combustion of the solid content can be used instead of the fuel cell. In this case, by adjusting the amount of oxygen gas to be supplied, the capacity of hydrogen gas is reduced, but the thermal efficiency and the profit efficiency of hydrogen can be balanced. Oxygen gas is supplied to the bubbling fluidized bed 108 together with the water vapor S via the wind box 103. The oxygen gas contributes to the partial combustion of the solid content in the bubbling fluidized bed 108 and supplies the heat required for gasification of the solid content in the bubbling fluidized bed 108.

FIG. 4 shows a flow sheet of electric power-hydrogen co-production that co-produces electric power and hydrogen. The numerical values in the figure indicate the energy at each stage when the energy of coal is 100, and the numerical values in parentheses indicate the energy ratio and the exergy ratio. As shown in FIG. 4, power-hydrogen production has no energy loss.

When hydrogen is converted into electrical energy using a fuel cell, 17% of the calorific value of hydrogen is generated as heat. If hydrogen is produced by reducing water with coal, petroleum, biomass, and natural gas using this heat, heat generation can be suppressed and power generation efficiency can be improved.

The power generation device according to the present invention can be suitably used as a power generation device in a power plant of a commercial power system. Further, it can be suitably used as a power generation device in a private power generation facility or a power generation device connected to a microgrid.

G Raw material S Steam 2 Flow layer gasifier 3 Windbox 4 Dispersion plate 5 Flow medium 6 Fuel cell 7 Downward flow moving layer 8 Bubbling flow layer 9 Partition member 10 Free board part 11 Raw material input part 12 Lower opening 13 Upper space 14 Flow control means 21 Tar decomposition device 22 Gas cleaning device (dust collector)
23 Shift Reactor 24 IDF
25 CO2 Separator 26 Hydrogen Separator 27 Hydrogen Tank

In order to achieve the above-mentioned object, the hydrogen production apparatus according to the present invention heats a raw material to generate a descending fluidized bed that separates into volatile components and solids, and heats the solids to generate a first produced gas. It has a bubbling fluidized bed, and has an internal circulation type fluidized bed in which the downward flow moving layer and the bubbling fluidized bed are separated by a partition member. In the hydrogen production apparatus according to the present invention, the solid content heating means is arranged in the bubbling fluidized bed.

It has a downflow moving layer that heats raw materials to separate them into volatile and solid contents, and a bubbling fluidized bed that heats the solids to generate a first produced gas, and has the downflow moving layer and the bubbling flow. An internal circulation type bubbling fluidized bed in which the layer is separated by a partition member may be provided, and a heating means may be arranged in the bubbling fluidized bed to form a hydrogen production apparatus.

Claims (16)

A downflow moving layer that heats the raw material to separate it into volatile and solid components,
It has a bubbling fluidized bed that heats the solid content to generate the first produced gas.
A hydrogen production apparatus including an internal circulation type fluidized bed in which the descending moving bed and the bubbling fluidized bed are separated by a partition member. The hydrogen production apparatus according to claim 1, wherein the solid content heating means is arranged in the bubbling fluidized bed. The hydrogen production apparatus according to claim 2, wherein the bubbling fluidized bed is fluidized by supplying water vapor to the bubbling fluidized bed. The hydrogen production apparatus according to claim 3, wherein the heat required for gasifying the solid content is not based on the partial combustion of the solid content but by the heating means. The hydrogen production apparatus according to claim 4, wherein the heating means is a fuel cell. The hydrogen production apparatus according to claim 4, wherein the heating means is an electric heater. The hydrogen production apparatus according to claim 4, wherein the heating means is a tube heat exchanger. The hydrogen production apparatus according to any one of claims 5 to 7, wherein the water vapor can be supplied to the downward flow moving layer via the flow rate adjusting means. The hydrogen production apparatus according to claim 8, wherein the flow rate adjusting means is adjusted according to the output of the temperature detecting means provided in the descending flow moving layer. The hydrogen production apparatus according to claim 9, wherein air and oxygen are not supplied to the bubbling fluidized bed. The hydrogen production apparatus according to any one of claims 2 to 10, wherein the first produced gas and the second produced gas obtained by thermally decomposing the volatile matter are guided to a shift reactor to generate hydrogen gas. The hydrogen production apparatus according to claim 11, wherein a tar decomposition apparatus for removing the tar component contained in the first produced gas and the second produced gas is provided in front of the shift reactor. The hydrogen production apparatus according to claim 11, wherein hydrogen from the shift reactor is supplied to the fuel cell and can be taken out of the system. The hydrogen production apparatus according to claim 13, wherein the steam generated during power generation of the fuel cell is supplied to the bubbling fluidized bed. The hydrogen production apparatus according to any one of claims 5 to 14, wherein the heat required for gasification of the raw material and the solid content is not due to partial combustion of the raw material and the solid content. The hydrogen production apparatus according to claim 1, wherein the first produced gas is generated by heat generated by partial combustion of the solid content by oxygen gas supplied to the bubbling fluidized bed.

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