JP2007223843A - Apparatus and method for producing hydrogen - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an apparatus for producing hydrogen in which the availability of energy can be enhanced and equipment can be simplified. <P>SOLUTION: The apparatus for producing hydrogen has a raw material supply system 104 for supplying mixed steam containing a fuel gas and raw material steam and a reformer 103 for forming hydrogen by steam reforming the mixed steam introduced from the raw material supply system 104 by heating the mixed steam with steam for heating, produced in a steam production utilization facility 101. The reformer 103 is equipped with: a plurality of reaction tubes 111 into each of which the mixed steam is introduced; a catalyst 115 which is provided in each reaction tube 111 and facilitates steam reforming of the mixed steam to form hydrogen; a heat medium oil 113 which is stored in each shell 112 and is brought into contact with the outer surface of each reaction tube 111, and steam tubes 114 which are each immersed in the heat medium oil 113 and heat the heat medium oil 113 by introducing the steam for heating, produced in the steam production utilization facility 101. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a hydrogen production apparatus and a production method for producing hydrogen as a heating source of a hydrogen production plant by partially diverting water vapor from an existing power plant or the like.

In the recent electric power industry, diversification of fuels has been researched and developed from the viewpoints of energy saving to cope with fossil fuel depletion and environmental conservation associated with increased concentrations of CO ₂ and NOx. There is.

  As this hydrogen gas utilization technology, for example, there are a fuel cell power generation system and a hydrogen combustion power plant. The former is known to generate electric energy directly by an electrochemical reaction between a fuel such as hydrogen and an oxidant typified by oxygen (see, for example, Patent Document 1). In the latter, high-pressure hydrogen gas and pure oxygen gas are burned to generate high-temperature water vapor, and the generated high-temperature water vapor is expanded by a turbine, and the generator is driven by the power generated at that time to generate power. (For example, refer to Patent Document 2).

As mentioned above research, the former, NOx in the latter both, SOx, from the standpoint of a very available clean energy that does not generate environmental pollutants and greenhouse gases such as CO _2, as part of the new energy promotion policy for the 21st century The results of are attracting attention.

  By the way, it has been proposed that hydrogen supplied as fuel to a fuel cell power plant or a hydrogen combustion power plant is produced by electrolysis of water. In hydrogen production by electrolysis of water, most of the necessary cost is electric power. In current nuclear power plants and thermal power plants, only about 50% of fission energy exchanged for heat and fuel energy such as oil and natural gas is converted into electric power. In particular, the heat utilization efficiency in a nuclear power plant is about 30%. For this reason, in the hydrogen production by electrolysis of water, there is a problem and inconvenience that the efficiency of energy use is extremely poor, leading to high costs.

On the other hand, oxygen-containing hydrocarbons such as methanol and dimethyl ether can be steam reformed at a low temperature, and therefore, when used as a hydrogen generation source in hydrogen production, it is advantageous in terms of cost. Methanol, dimethyl ether, ethanol, and the like are relatively large because they are produced from methane in small and medium gas fields, carbon dioxide, and gas fields with a high CO ₂ content. A methanol reforming reaction apparatus proposed by paying attention to such a point is known (for example, see Patent Document 3).

This methanol reforming reaction apparatus performs a reaction while heating a mixed vapor of methanol and water with a heat medium oil in the presence of a catalyst. This is a technology that can reduce the size of the reformer. In this apparatus, a U-shaped reaction tube is installed, and heat medium oil is supplied to the upper part on the barrel side and extracted from the lower part. The reaction tube is heated while circulating the heat medium oil heated by an external heater with a pump. As another example, a technique is also known in which a raw material evaporator, a reforming reactor, an electric heating heater, a catalytic combustor, and a stirrer are placed in the same heat medium oil tank and heated while stirring with a stirrer.
JP-A-6-140065 Japanese Patent Laid-Open No. 11-36820 Japanese Patent Laid-Open No. 3-60401

  In the conventional methanol reforming reaction apparatus mentioned above, it reacts, heating the mixed vapor | steam of methanol and water with heat medium oil in presence of a catalyst. Since oxygen-containing hydrocarbons such as methanol and dimethyl ether can be steam-reformed at low temperatures, they are advantageous in terms of cost when producing hydrogen.

  However, in this methanol reforming reaction apparatus, it is necessary to provide a heating device, a circulation pump, piping and the like outside in order to heat and circulate the heat medium oil. The introduction of the methanol reforming reaction apparatus has a problem that the facilities related to the methanol reforming reaction apparatus are increased and the installation space is increased.

  On the other hand, in order to omit the above circulating pump and piping, a technology in which a raw material evaporator, a reforming reactor, an electric heating heater, a catalytic combustor and a stirrer are placed in the same heat medium oil tank and heated while stirring with a stirrer Has been proposed.

  However, even in this case, a heating device such as a heater or a catalytic combustor and a circulation device such as a stirrer are necessary, and there is a problem that the equipment is increased in size.

  The present invention has been made in order to solve the above-mentioned problems, and is intended to improve energy utilization efficiency and simplify equipment by partially using steam from an existing power plant or the like as a heating source for a hydrogen production plant. An object of the present invention is to provide a hydrogen production apparatus and a production method that can perform the above-described process.

  In order to achieve the above object, the present invention provides a raw material supply system that supplies a mixed steam containing fuel gas and raw material steam, and a steam for heating that is produced from the mixed steam introduced from the raw material supply system in a steam production facility. A hydrogen production apparatus comprising: a reformer that generates hydrogen by steam reforming and steam, wherein the reformer is provided in the reaction tube and a plurality of reaction tubes that introduce the mixed steam. A catalyst that promotes hydrogen generation by steam reforming the mixed steam; a shell including the reaction tube; and a heat medium oil stored in the shell and in contact with at least a part of the outer surface of the reaction tube; And a steam pipe that heats the heat medium oil by introducing the steam for heating produced in the water vapor production and utilization facility by being immersed in the heat medium oil.

  In order to achieve the above object, the present invention provides a raw material supply system for supplying a mixed steam containing fuel gas and raw material steam, and a steam for heating produced from the raw material supply system in the steam production and utilization facility using the mixed steam introduced from the raw material supply system. And a reformer for generating hydrogen by steam reforming to produce hydrogen, wherein the reformer is provided in a plurality of outer tubes into which the mixed steam is introduced and in the outer tubes Provided in a reaction tube that forms a double tube including an inner tube through which the generated hydrogen flows, and an annular gap formed between the outer tube and the inner tube, steam reforming the mixed steam promotes hydrogen generation Catalyst, a shell including the reaction tube, a heat medium oil stored in the shell and in contact with at least a part of the outer surface of the outer tube, and immersed in the heat medium oil and used for the production of water vapor Introducing heating steam produced at the facility Te is characterized in that it comprises a steam pipe for heating the thermal oil.

  According to the hydrogen production apparatus and production method of the present invention, it is possible to improve energy utilization efficiency and simplify equipment by partially diverting water vapor from an existing power plant or the like as a heating source for a hydrogen production plant. .

  Hereinafter, embodiments of a hydrogen production apparatus and a production method according to the present invention will be described with reference to the drawings. Here, the same or similar parts are denoted by common reference numerals, and redundant description is omitted.

  FIG. 1 is a configuration diagram showing a schematic configuration of the hydrogen production apparatus according to the first embodiment of the present invention.

  As shown in the figure, the hydrogen production apparatus is configured as a hydrogen production plant 102 connected to a steam production utilization facility 101. Hydrogen is generated by steam reforming the fuel in the hydrogen production plant 102 using the steam thermal energy of the steam production utilization facility 101.

  The steam production utilization facility 101 can be exemplified by a power plant or a waste incineration facility, for example. This power plant is a facility that generates high-pressure and high-temperature steam and generates electricity by driving a generator with the energy. In particular, large-scale facilities are equipped with a boiler that uses heat generated when garbage is incinerated (combusted), and steam produced by the boiler is used for a hot water pool, heating, and the like. In these power plants, waste incineration facilities, etc., water vapor after use is discharged or returned to water by a condenser and reused. Therefore, the water vapor produced and used in these facilities often has surplus energy.

  The hydrogen production plant 102 includes a reformer 103, a raw material supply system 104 that supplies a raw material that is a mixed steam of fuel and water, and a product gas recovery system 105.

  The raw material supply system 104 includes a fuel supply device 106 including a fuel tank such as ethanol and dimethyl ether, a preheater (not shown) that is gasified and preheated, and the like. In addition, a raw water vapor supply device 107 provided with a water tank for storing the raw water, a pump for supplying the stored raw water, and a water evaporator (not shown) for evaporating the supplied raw water is installed. ing. Further, a mixing unit 108 for introducing the fuel gas and the raw material water vapor to generate mixed steam is provided. Further, the generated gas recovery system 105 is provided with a device (not shown) for separating and recovering hydrogen gas generated by reforming the mixed steam and other generated gases to purify the hydrogen gas. Yes.

  Between the steam production / utilization facility 101 and the reformer 103, a steam extraction pipe 109 for extracting part or all of the steam produced in the steam production / utilization facility 101 and heating the reformer 103, Steam return pipes 110 for returning steam that has been heated in the reformer 103 are connected to each other.

  The reformer 103 includes a plurality of reaction tubes 111 and a shell 112 that includes the reaction tubes 111. Heat medium oil 113 is stored in the shell 112, and the heat medium oil 113 is in contact with at least a part of the outer surface of the reaction tube 111. In order to heat the heat medium oil 113, a steam pipe 114 is immersed in the heat medium oil 113. The steam extraction pipe 109 and the steam return pipe 110 are connected to the steam pipe 114 so that the steam for heating extracted from the steam production utilization facility 101 flows. The reaction tube 111 is filled with a catalyst 115 synthesized, for example, Cu—Zn or the like.

  In the present embodiment formed as described above, the high-temperature steam branched and extracted from the steam production utilization facility 101 is introduced into the reformer 103 via the steam extraction pipe 109. The introduced high-temperature water vapor exchanges heat with the heat medium oil 113 stored in the shell 112 via the steam pipe 114 to heat the heat medium oil 113. The steam after heating is returned to the steam production utilization facility 101 through the steam return pipe 110.

  On the other hand, the fuel supplied from the fuel supply device 106 of the raw material supply system 104, for example, oxygen-containing hydrocarbons such as ethanol and dimethyl ether is gasified by the fuel supply device 106. Further, the water introduced into the raw material steam supply device 107 of the raw material supply system 104 is vaporized by the raw material steam supply device 107. The fuel gas such as ethanol or dimethyl ether and the raw material water vapor are mixed in the mixing unit 108 to be mixed vapor. This mixed steam is supplied into the reaction tube 111 of the reformer 103.

  The supplied mixed steam is heated while passing through the voids of the packed bed of the catalyst 115 in the reaction tube 111 to perform a reforming reaction to generate hydrogen gas. For example, when the fuel is dimethyl ether, hydrogen gas is generated by performing a reforming reaction with water vapor as shown in the following formula (1).

CH ₃ OCH ₃ + 3H ₂ O → 6H ₂ + 2CO ₂ (1)
The hydrogen gas generated in this manner contains carbon dioxide CO ₂ and is separated and purified by the product gas recovery system 105 and recovered.

  Since the reaction represented by the above formula (1) is an endothermic reaction, it is necessary to continuously apply a predetermined amount of heat in order to continue this reforming reaction. As described above, the catalyst 115 and the mixed gas in the reaction tube 111 are heated by receiving heat from the heat medium oil 113 heated with the high-temperature steam in the steam production utilization facility 101. As the heat medium oil, for example, high boiling point high temperature heat medium oil such as Barrel Therm 400 (trade name) is used. The barrel thermo 400 can be used at a temperature of 300 ° C. or higher, has good thermal conductivity, has a large specific heat, and has a moderate temperature fluctuation, thereby enabling efficient and stable heating.

  In the system of the steam extraction pipe 109, when the temperature necessary for the reaction generation is insufficient, a heater that compensates for the shortage can be installed. Further, the system outside the reformer 103 requires a valve for adjusting the flow rate or for closing, but the illustration is omitted.

  According to the present embodiment, most of the energy required for hydrogen production can be effectively utilized by using the thermal energy of the steam generated from the steam production utilization facility 101 for the reformer 103 of the hydrogen production plant 102. Furthermore, since the used steam is returned again to the steam production and use facility 101, the thermal energy of the steam can be used effectively without waste. Thus, the energy efficiency of the steam production and utilization facility 101 can be further improved.

  Moreover, since the heating medium oil 113 is used, efficient and stable heating is possible. Further, high-pressure steam produced at the steam production / utilization facility 101 is led into the shell 112 through a pipe 114. Thus, since the pressure boundary is the pipe 114, the safety is high and the shell 112 does not need to be a high-pressure container, so the container wall thickness can be reduced and the weight can be reduced. Can be achieved.

  FIG. 2 is a configuration diagram showing a schematic configuration of the hydrogen production apparatus according to the second embodiment of the present invention. This figure shows a modified example of the configuration of the reformer 103 in FIG. 1, and the same or similar parts as in FIG.

  As shown in the figure, the reformer 103 of the hydrogen production apparatus includes a plurality of reaction tubes 111 and a shell 112 that includes the reaction tubes 111. Heat medium oil 113 is stored in the shell 112, and the heat medium oil 113 heats the heat medium oil 113 in contact with at least a part of the outer surface of the reaction tube 111 in order to heat the heat medium oil 113. A steam pipe 114 is immersed in the oil 113.

  The steam pipes 114 are installed in a lower layer portion of the first steam pipe 114 </ b> A installed in the space region between the reaction tubes 111 and the heat medium oil 113 stored in the lower part of the shell 112. And a second steam pipe 114B.

  The steam extraction pipe 109 is connected to the upstream side of one end of the first steam pipe 114A. The reformer 103 is heated by extracting part or all of the high-temperature steam produced in the steam production / utilization facility 101 through the steam extraction pipe 109. The steam extraction pipe 109 is also branched and connected to the upstream side of one end of the second steam pipe 114B, and high-temperature steam produced at the steam production and utilization facility 101 is introduced into the reformer 103.

  The steam return pipe 110 is connected to the downstream side of the other end of the first steam pipe 114A so that the steam that has finished the heating is returned to the steam production utilization facility 101. Further, the downstream pipe at the other end of the second steam pipe 114A joins and is connected to the steam return pipe 110, and the steam after heating is returned to the steam production utilization facility 101.

  In the present embodiment, the high-temperature steam branched and extracted from the steam production / utilization facility 101 is supplied to the reformer 103 via the steam extraction pipe 109. The supplied high-temperature steam exchanges heat with the heat medium oil 113 stored in the shell 112 through the steam pipe 114A and heats it. The water vapor that heats the heat medium oil 113 is returned to the water vapor production and utilization facility 101 via the vapor return pipe 110. Further, the steam pipe 114B disposed in the lower layer portion of the stored heat medium oil 113 is also branched from the steam extraction pipe 109 and supplied with high-temperature steam. The supplied high-temperature steam heats the lower layer portion of the heat medium oil 113, joins the steam return pipe 110, and returns to the steam production utilization facility 101.

On the other hand, a mixed gas of fuel gas such as ethanol or dimethyl ether and raw material steam is supplied from a raw material supply system 104 into a reaction tube 111 built in the reformer 103. This mixed gas undergoes a reforming reaction while passing through the void portion of the packed bed formed from the catalyst 115 in the reaction tube 111 to generate hydrogen gas. Since the generated hydrogen gas contains carbon dioxide CO ₂ , it is separated and purified by the product gas recovery system 105 and recovered.

  Since the reforming reaction is an endothermic reaction, it is necessary to continuously apply a predetermined amount of heat in order to continue the reforming reaction. For this purpose, the catalyst 115 and the mixed gas in the reaction tube 111 are heated by receiving heat from the heat medium oil 113 heated with the high-temperature steam in the steam production utilization facility 101.

  On the other hand, the temperature of the steam in the steam pipe 114A becomes lower as it goes downstream due to heat exchange, and the temperature of the lower layer portion of the stored heat medium oil 113 becomes lower and stratification can be performed at a lower temperature. There was a fear. For this purpose, a steam pipe 114B is provided in the lower layer portion of the heat medium oil 113, and the lower layer portion is heated by flowing heating steam. Due to the heating by the steam pipe 114B, the temperature of the lower layer portion of the heat medium oil 113 rises, the specific gravity of the heat medium oil becomes light, natural convection occurs, and the temperature uniformity is maintained. As this heat medium oil, for example, a high boiling point high temperature heat medium oil such as Barrel Therm 400 (trade name) is used, so it can be heated to 300 ° C. or higher, has good thermal conductivity, has a large specific heat, and a high temperature. Fluctuation is gradual. For this reason, efficient and stable heating is possible.

  According to the present embodiment, most of the energy required for hydrogen production can be effectively utilized by using the thermal energy of the steam generated from the steam production utilization facility 101 for the reformer 103 of the hydrogen production plant 102. Furthermore, since the used steam is returned again to the steam production and use facility 101, the thermal energy of the steam can be used effectively without waste. Thus, the energy efficiency of the steam production and utilization facility 101 can be further improved.

  Further, not only a plurality of first steam pipes 114 </ b> A are installed between the reaction pipes 111, but also a second steam pipe 114 </ b> B is installed in the lower layer portion of the stored heat medium oil 113. By providing the second steam pipe 114B, the temperature of the lower layer portion of the heat medium oil 113 rises, the specific gravity of the heat medium oil 113 becomes light, natural convection occurs, and the temperature uniformity can be maintained. Well stable heating becomes possible.

  FIG. 3 is a structural diagram showing a schematic structure of a modification of the reformer 103 of FIG. In this figure, plate fins 116 are added to the reformer 103 in FIG. 2, and the same or similar parts as in FIG.

  As shown in the figure, a plate fin 116 for promoting heat transfer is provided on at least one of the outer surfaces of the reaction tube 111 and the steam tube 114 built in the reformer 103 or shared with the outer surface. ing. Here, the plate fin 116 is attached to the outer surface of the first steam pipe 114A. Here, the plate fin 116 shows an example in which a plate fin 316 shared by the reaction tube 111 and the steam tube 114A is installed. It is also possible to improve heat transfer characteristics by providing another plate fin 116 in the steam pipe 114B.

  According to the present embodiment, by providing the plate fin 116 shared by the steam pipe 114A and the reaction pipe 111, the heat transfer is improved by improving the heat transfer area, and further the heat transfer performance by the heat conduction from the steam pipe 114A. Can be improved.

  FIG. 4 is a structural diagram showing a partially enlarged view of a steam pipe 114A and its peripheral part of another modification of the reformer 103 of FIG. In this figure, the flow path hole 117 is added to the plate fin 116 of FIG. 3, and the same or similar parts as in FIG.

  As shown in this figure, plate fins 116 for promoting heat transfer are provided in common on the outer surfaces of the reaction tube 111 and the steam tube 114A built in the reformer 103. The plate fin 116 is provided with a flow path hole 117 through which the heat medium oil 113 flows.

  According to the present embodiment, by providing the channel hole 117 in the plate fin 116, it is possible to promote the flow of the heat medium oil 113 and the natural circulation in the reformer 103. For this reason, since a circulation device such as a circulation pump for the heat medium oil 117 is not required, the hydrogen production device can be simplified and the safety can be improved. Furthermore, by providing the heat transfer performance plate fin 116 shared by the heating steam tube and the reaction tube, the heat transfer performance related to hydrogen production is improved, so that the hydrogen generation efficiency can be improved.

  FIG. 5 is a structural diagram showing a partially enlarged view of a steam pipe 114A and its peripheral portion of still another modified example of the reformer 103 of FIG. In this figure, a notch channel portion 118 is added to the plate fin 116 of FIG. 3, and the same or similar parts as in FIG.

  As shown in this figure, plate fins 116 for promoting heat transfer are provided in common on the outer surfaces of the reaction tube 111 and the steam tube 114A built in the reformer 103. The plate fin 116 is provided with a notch channel portion 118 through which the heat medium oil 113 flows. Further, by providing a partition plate (not shown) or the like, the convection of the heat medium oil 113 can be promoted so that the upward flow and the downward flow of the heat medium oil 113 do not interfere with each other.

  According to the present embodiment, by providing the notch channel portion 118 in the plate fin 116, the heating of the heat medium oil 117 and the flow by natural circulation can be promoted in the reformer 103. For this reason, since a circulation device such as a circulation pump for the heat medium oil 117 is not required, the hydrogen production device can be simplified and the safety can be improved. Furthermore, by providing the heat transfer performance plate fin 116 shared by the heating steam tube and the reaction tube, the heat transfer performance related to hydrogen production is improved, so that the hydrogen generation efficiency can be improved.

  FIG. 6 is a configuration diagram showing a schematic configuration of the hydrogen production apparatus according to the third embodiment of the present invention. This figure shows a modified example of the configuration of the reformer 103 in FIG. 1, and the same or similar parts as in FIG.

  As shown in the figure, the reformer 103 has a plurality of reaction tubes 411 and a shell 412 that includes the reaction tubes 411. Heat medium oil 113 is stored in the shell 412, and the heat medium oil 113 is in contact with at least a part of the outer surface of the reaction tube 411. In order to heat the heat medium oil 113, a steam pipe 414 is immersed in the heat medium oil 113. The steam extraction pipe 109 and the steam return pipe 110 are connected to the steam pipe 414 so that the heating steam extracted from the steam production / utilization facility 101 flows.

  The reaction tube 411 is filled with a catalyst 115 synthesized, for example, Cu—Zn or the like. Moreover, as the heat medium oil 113, for example, there is a high boiling point high temperature heat medium oil such as Barrel Therm 400 (trade name), which can be used at a temperature of 300 ° C. or higher.

  The reaction tube 411 constitutes a bayonet type double tube. The reaction tube 411 includes an outer tube 411A and an inner tube 411B. The outer tube 411A is fixed to the tube plate 419 with the lower end closed and the upper end opened. The inner tube 411B is open at both ends, and the upper end is fixed to the tube plate 420.

  The shell 412 is divided into three rooms 412A, a room 412B, and a room 412C by a tube plate 419 and a tube plate 420. The heat medium oil 113 is stored in the room 412A. A steam pipe 414 is immersed in the heat medium oil 113.

  The room 412B is filled with a mixed gas of reforming raw materials supplied from the raw material supply system 104. This chamber 412B forms a manifold of mixed gas for branching and supplying the mixed gas to the outer tube 411A constituting the plurality of reaction tubes 411.

  The chamber 412C is a product gas manifold in which product gas such as hydrogen gas produced by the reforming reaction is collected via a plurality of inner tubes 411B constituting the plurality of reaction tubes 411. The product gas collected in the room 412C is led to the product gas recovery system 105 and separated and purified.

  Further, the annular gap formed by the outer tube 411A and the inner tube 411B of the reaction tube 411 is filled with the catalyst 115. The packed bed of the catalyst 115 has a gap so that the mixed gas flows. In the annular gap of the reaction tube 411, for example, a perforated receiving plate 421 such as a mesh is installed. By providing the receiving plate 421, a catalyst non-filling portion 411C is formed in the lower region of the annular gap of the reaction tube 411.

  In the present embodiment, the high-temperature steam branched and extracted from the steam production / utilization facility 101 is introduced into the reformer 103 via the steam extraction pipe 109. This high-temperature steam is heated by exchanging heat with the heat medium oil 113 stored in the shell 412 via the steam pipe 414. The steam that heats the heat medium oil 113 is returned to the steam production utilization facility 101 via the steam return pipe 110.

  On the other hand, for example, a mixed gas containing fuel gas and raw water vapor is supplied from the raw material supply system 104 into the room 412B. As the fuel gas, an oxygen-containing hydrocarbon gas such as ethanol or dimethyl ether is used. The mixed gas supplied into the chamber 412B branches and flows to outer tubes 411A constituting a plurality of reaction tubes. In the outer tube 411A, the mixed gas receives heat from the heat medium oil 113 in the process of passing through the voids of the packed bed of the catalyst 115. For example, when the fuel is dimethyl ether, hydrogen gas is generated by performing a reforming reaction with high-temperature steam as shown in the above formula (1).

  The product gas generated by the reforming reaction is U-turned at the lower part of the outer tube 411A, collected in the room 412C via the inner tube 411B, and led to the product gas recovery system 105. On the other hand, since it is an endothermic reaction in the catalyst 115 layer, the heat medium oil 113 receives the amount of heat necessary for this reforming reaction.

Furthermore, since the catalyst non-filling portion 411C that does not perform the endothermic reaction is provided at the lower portion of the outer tube 411A, the product gas is reheated in this portion. This reheated product gas can be heated from the inside of the layer of the catalyst 115 by exchanging heat when flowing through the inner pipe 411B, so that a larger amount of heat can be given to the reforming reaction. it can. This gas mainly consists of hydrogen gas, but contains carbon dioxide CO ₂ , and is separated and purified by the product gas recovery system 105 and recovered.

  According to the present embodiment, since the heat energy of steam generated from the steam production utilization facility 101 can be used for the reformer of the hydrogen production plant, most of the energy required for hydrogen production can be effectively utilized and further utilized. After that, it is returned to the steam production facility so that it can be used effectively without waste. For this reason, the energy efficiency of a steam production utilization facility can be improved further. Moreover, since heat is exchanged using the heating medium oil, more efficient and stable heating is possible.

  Furthermore, the high-pressure steam produced in the steam production / utilization facility is led into the shell through a pipe. For this reason, since the pressure boundary is piping, safety is high, and the shell does not need to be a high-pressure container, and the thickness of the container can be reduced and the weight can be reduced, greatly reducing the metal resources used. can do. Also, by combining heating from the outside of the catalyst packed bed with heat transfer oil and reheating of the product gas from the inside of the packed catalyst bed, the heat exchange efficiency of the reformer can be improved and efficient hydrogen production is possible It becomes.

  FIG. 7 is a configuration diagram showing a schematic configuration of the hydrogen production apparatus according to the fourth embodiment of the present invention. This figure shows a modified example of the configuration of the reformer 103 in FIG. 6, and the same or similar parts as in FIG.

  As shown in the figure, the reformer 103 of the hydrogen production apparatus includes a plurality of reaction tubes 411 and a shell 412 that includes the reaction tubes 411. Heat medium oil 113 is stored in the shell 412, and the heat medium oil 113 is in contact with at least a part of the outer surface of the reaction tube 411. In order to heat the heat medium oil 113, a steam pipe 414 is immersed in the heat medium oil 113.

  The steam pipe 414 includes a plurality of first steam pipes 414A installed in a space region between the reaction tubes 411, and a second steam pipe 414 installed in a lower layer portion of the heat medium oil 113 stored in the shell 412. The steam pipe 414B.

  The steam extraction pipe 109 is connected to the upstream side of one end of the first steam pipe 414A. The reformer 103 is heated by extracting part or all of the high-temperature steam produced in the steam production / utilization facility 101 through the steam extraction pipe 109. The steam extraction pipe 109 is also branched and connected to the upstream side of one end of the second steam pipe 414B, and high-temperature steam produced in the steam production and utilization facility 101 is introduced into the reformer 103.

  The steam return pipe 110 is connected to the downstream side of the other end of the first steam pipe 414A so that the steam that has been heated is returned to the steam production utilization facility 101. The downstream pipe at the other end of the second steam pipe 414B joins and is connected to the steam return pipe 110, and the heated steam is returned to the steam production utilization facility 101.

  In the present embodiment, the high-temperature steam branched and extracted from the steam production / utilization facility 101 is supplied to the reformer 103 via the steam extraction pipe 109. The supplied high temperature steam exchanges heat with the heat medium oil 113 stored in the shell 412 through the steam pipe 414A and heats it. The water vapor that heats the heat medium oil 113 is returned to the water vapor production and utilization facility 101 via the vapor return pipe 110. Further, the steam pipe 414B disposed in the lower layer portion of the stored heat medium oil 113 is also branched from the steam extraction pipe 109 and supplied with high-temperature steam. The supplied high-temperature steam heats the lower layer portion of the heat medium oil 113, joins the steam return pipe 110, and returns to the steam production utilization facility 101.

On the other hand, a mixed gas of fuel gas such as ethanol or dimethyl ether and raw material water vapor is supplied from the raw material supply system 104 into the outer tube 411 A constituting the reaction tube 411 built in the reformer 103. This mixed gas undergoes a reforming reaction while passing through the voids of the packed bed formed from the catalyst 115 in the outer tube 411A to generate hydrogen gas. The product gas generated by the reforming reaction is U-turned at the lower part of the outer tube 411A, collected in the room 412C via the inner tube 411B, and led to the product gas recovery system 105. Since the generated hydrogen gas contains carbon dioxide CO ₂ , it is separated and purified by the product gas recovery system 105 and recovered.

  Since the reforming reaction is an endothermic reaction, it is necessary to continuously apply a predetermined amount of heat in order to continue the reforming reaction. For this reason, the catalyst 115 and the mixed gas in the outer pipe 411A constituting the reaction pipe 411 are heated by receiving heat from the heat medium oil 113 heated with the high-temperature steam in the steam production utilization facility 101. Yes.

  On the other hand, the temperature of the steam in the steam pipe 414A becomes lower as a result of heat exchange, and the temperature of the lower layer of the stored heat medium oil 113 becomes lower and stratification can be performed at a lower temperature. There was a fear. For this purpose, a steam pipe 414B is provided in the lower layer portion of the heat medium oil 113, and the lower layer portion is heated by flowing heating steam. Due to the heating by the steam pipe 414B, the temperature of the lower layer portion of the heat medium oil 113 rises, the specific gravity of the heat medium oil becomes light, natural convection occurs, and the temperature uniformity is maintained. As this heat medium oil, for example, a high boiling point high temperature heat medium oil such as Barrel Therm 400 (trade name) is used, so it can be heated to 300 ° C. or higher, has good thermal conductivity, has a large specific heat, and a high temperature. Since the fluctuation is gradual, efficient and stable heating is possible.

  In the present embodiment formed as described above, the high-temperature steam branched and extracted from the steam production and utilization facility 101 is introduced into the reformer 103 through the steam extraction pipe 109. The introduced high-temperature water vapor exchanges heat with the heat medium oil 113 stored in the shell 412 via the steam pipe 414A to heat the heat medium oil 113. The heated steam is returned to the steam production / utilization facility 101 through the steam return pipe 110.

  Further, the high-temperature steam branched from the steam extraction pipe 109 is also introduced into the steam pipe 414B disposed in the lower layer portion of the stored heat medium oil 113. The introduced high-temperature steam heats the lower layer portion of the heat medium oil 113, joins the steam return pipe 110, and returns to the steam production utilization facility 101.

  On the other hand, a fuel supplied from the raw material supply system 104, for example, a mixed gas of oxygen-containing hydrocarbon gas such as ethanol and dimethyl ether and raw material water vapor is supplied into the room 412B. The supplied mixed gas is divided and introduced into the outer tubes 411A constituting the plurality of reaction tubes 411. The introduced mixed gas is heated by receiving heat from the heat medium oil 113 while passing through the voids of the packed bed of the catalyst 115.

  For example, when the steam fuel is dimethyl ether, hydrogen gas is generated by performing a reforming reaction with high-temperature steam as shown in the above formula (1). The generated product gas is U-turned at the lower part of the outer tube 411A, collected in the room 412C via the inner tube 411B, and led to the product gas recovery system 105.

Since the reforming reaction in the packed bed of the catalyst 115 is an endothermic reaction, the amount of heat necessary for this reaction is received from the heat medium oil 113. Furthermore, since the catalyst non-filling portion 411C that does not perform the endothermic reaction is provided in the lower portion of the outer tube 411A, the product gas is reheated in this portion. The reheated product gas is also heated from the inside of the packed bed of the catalyst 115 when flowing in the inner pipe 411B, so that a larger amount of heat can be given to the reforming reaction section. This product gas is mainly composed of hydrogen gas but contains carbon dioxide CO ₂ , and is separated and purified by the product gas recovery system 105 and recovered.

  On the other hand, the temperature of the steam in the steam pipe 414 </ b> A becomes lower as it goes to the downstream side due to heat exchange, and the temperature of the lower layer portion of the heat medium oil 113 becomes lower, which may reduce the reforming reaction efficiency. For this purpose, by disposing the steam pipe 414B in the lower layer portion of the heat medium oil 113, the heating steam flows through the lower layer portion and is heated. By raising the temperature of this lower layer part, the specific gravity of the heat medium oil 113 is reduced, natural convection is promoted, and temperature uniformity is maintained.

  According to the present embodiment, most of the energy required for hydrogen production can be effectively utilized by using the thermal energy of the steam generated from the steam production utilization facility 101 for the reformer 103 of the hydrogen production plant 102. Furthermore, since the used steam is returned again to the steam production and use facility 101, the thermal energy of the steam can be used effectively without waste. Thus, the energy efficiency of the steam production and utilization facility 101 can be further improved.

  In addition, a plurality of first steam pipes 414A are installed between the outer pipes 411A, and a second steam pipe 414B is installed in the lower layer portion of the stored heat medium oil 113. By providing the second steam pipe 414B, the temperature of the lower layer portion of the heat medium oil 113 is increased, the specific gravity of the heat medium oil 113 is reduced, natural convection is promoted, and the temperature uniformity can be maintained. Stable heating is possible.

  FIG. 8 is a structural diagram showing a schematic structure of a modified example of the reformer 103 of FIG. In this figure, plate fins 616 are added to the reformer 103 of FIG. 7, and the same or similar parts as in FIG.

  As shown in this figure, the outer tube 411A and the steam tube 414A constituting the reaction tube 411 built in the reformer 103 are shared with at least one of the outer surfaces or the outer surface to promote heat transfer. Plate fins 616 are provided. Here, a plate fin 616 is attached to the outer surface of the first steam pipe 414A. Moreover, this plate fin 616 has shown the example which installed the plate fin 616 shared by the outer tube | pipe 411A and the steam pipe 414A. It is also possible to improve the heat transfer characteristics by providing another plate fin 616 in the steam pipe 414B.

  According to the present embodiment, by providing the plate fin 616 shared by the outer pipe 411A and the steam pipe 414A, the heat transfer is improved by improving the heat transfer area, and further the heat transfer performance by the heat conduction from the steam pipe 414A. Can be improved.

  FIG. 9 is a structural diagram showing a partially enlarged view of a steam pipe 414A and its peripheral part of another modification of the reformer 103 of FIG. In this figure, a plate hole 617 is additionally provided in the plate fin 616 of FIG. 8, and the same or similar parts as in FIG.

  As shown in the figure, plate fins 616 for promoting heat transfer are provided in common on the outer surfaces of the outer tube 411A and the first steam tube 414A constituting the reaction tube 411. The plate fins 616 are provided with flow passage holes 617 so that natural convection of the heat medium oil 113 is not impaired.

  According to the present embodiment, by providing the channel holes 617 in the plate fins 616, the heat of the heat medium oil 113 and the flow by natural circulation can be promoted in the reformer 103. For this reason, since a circulation device such as a circulation pump for the heat medium oil 113 is not required, the hydrogen production device is simplified and safety can be improved. Furthermore, by providing the heat transfer performance plate fins 616 shared by the heating steam pipe and the reaction pipe, the heat transfer performance related to hydrogen production is improved, so that the hydrogen generation efficiency can be improved.

  FIG. 10 is a structural diagram showing a partially enlarged view of a steam pipe and its peripheral part of still another modification of the reformer of FIG. In this figure, a notch channel portion 618 is additionally provided in the plate fin 616 of FIG. 8, and the same or similar parts as those in FIG.

  As shown in the figure, plate fins 616 for promoting heat transfer are provided in common on the outer surfaces of the outer tube 411A and the first steam tube 414A constituting the reaction tube 411. The plate fin 616 is provided with a notch channel portion 618 through which the heat medium oil 113 flows. Further, by providing a partition plate (not shown) or the like, the convection of the heat medium oil 113 can be promoted so that the upward flow and the downward flow of the heat medium oil 113 do not interfere with each other.

  According to the present embodiment, by providing the plate fin 616 with the notch flow path section 618, the heat of the heat medium oil 113 and the flow by natural circulation can be promoted in the reformer 103. For this reason, since a circulation device such as a circulation pump for the heat medium oil 113 is not required, the hydrogen production device is simplified and safety can be improved. Furthermore, by providing the heat transfer performance plate fins 616 shared by the heating steam pipe and the reaction pipe, the heat transfer performance related to hydrogen production is improved, so that the hydrogen generation efficiency can be improved.

  FIG. 11: is a block diagram which shows schematic structure of the hydrogen production apparatus of the 5th Embodiment of this invention. This figure shows a modification of the configuration of the raw material supply system in FIG. 1, and the same or similar parts as in FIG.

  As shown in the figure, the hydrogen production apparatus is configured by connecting a hydrogen production plant 102 to a steam production utilization facility 101. Hydrogen is generated by steam reforming the fuel in the hydrogen production plant 102 using the steam thermal energy of the steam production utilization facility 101. The steam production utilization facility 101 is, for example, a power plant or a waste incineration facility.

  The hydrogen production plant 102 includes a reformer 103, a raw material supply system 704 that supplies a mixed steam of fuel gas and raw material steam, and a product gas recovery system 105.

  The raw material supply system 704 includes a heat medium oil storage tank 727, an attached fuel tank 722, and a raw water supply system 724. The fuel tank 722 stores a fuel such as ethanol or dimethyl ether. The raw water supply system 724 includes a raw water tank that stores raw water, a feed water pump (not shown) that supplies raw water, and the like.

  The fuel stored in the fuel tank 722 is introduced into a fuel preheater 723 provided in the heat medium oil storage tank 727 and is gasified and preheated. The raw water stored in the raw water supply system 724 is supplied to a raw water evaporator 725 provided in the heat medium oil storage tank 727 and is evaporated. The fuel gas and the raw material steam are introduced into the mixing unit 726 and become mixed steam. This mixed steam is introduced into the reformer 103 via a pipe 729.

  Further, the heat medium oil 113 is stored in the heat medium oil storage tank 727. In the heat medium oil 113, the fuel preheater 723, the raw water evaporator 725, and the mixing unit 726 are immersed. A fuel heating steam pipe 728 is provided below the medium oil storage tank 727. The fuel heating steam pipe 728 is also immersed in the stored heat medium oil 113.

  In order to heat the heat medium oil 113 in the reformer 103 and the heat medium oil storage tank 727 by partially extracting the high-temperature steam produced in the steam production and use facility 101, the steam production and use facility 101 and the reformer 103 are heated. And a steam extraction pipe 109 is provided between the steam production facility 101 and the heat medium oil storage tank 727. In addition, a steam return pipe 110 for returning the heated steam to the steam production / utilization facility 101 is provided between the steam production / utilization facility 101 and the reformer 103, the steam production / utilization facility 101, the heat medium oil storage tank 727, Between the two.

  In the present embodiment, the high-temperature steam extracted from the steam production utilization facility 101 is branched and introduced into the reformer 103 and the heat medium oil storage tank 727 via the steam extraction pipe 109. The heated water vapor introduced into the heat medium oil storage tank 727 heats the heat medium oil 113 through the fuel heating steam pipe 728. The steam that has been heated is returned to the steam production utilization facility 101 via the steam return pipe 110.

  In the heat medium oil storage tank 727, the heated heat medium oil 113 heats the fuel preheater 723 to heat the fuel, and the water evaporator 725 is heated to generate raw water vapor, and further in the mixing unit 726. The mixed steam of fuel gas and raw material steam is heated. The heat medium oil 113 is circulated by natural convection in the heat medium oil storage tank 727 and heat-exchanged with the heated steam flowing in the fuel heating steam pipe 728.

  This heated mixed gas is introduced into the reformer 103 via the pipe 729 and reformed into hydrogen. The heated heat medium oil 113 is circulated by natural convection in the heat medium oil storage tank 727 and heat-exchanged with the heated steam flowing in the fuel heating steam pipe 728.

  The system related to the steam extraction pipe 109 may be provided with a heater that compensates for the shortage when the temperature required for reaction generation is insufficient. Further, a valve for adjusting the flow rate or closing the valve is attached to the system outside the reformer 103, but is omitted.

  According to the present embodiment, the heat energy of the steam generated from the steam production utilization facility 101 can be used for the reformer 103 of the hydrogen production plant 102, so that most of the energy required for hydrogen production can be effectively utilized, and After use, it is returned to the steam production / utilization facility 101 so that it can be used effectively without waste. For this reason, the energy efficiency of the steam production utilization facility 101 can be further improved.

  Further, since the heating medium oil 113 is used, efficient and stable heating can be performed. Furthermore, since the high-pressure steam produced at the steam production / utilization facility 101 is introduced into the shell 112 by the pipe 109, the pressure boundary is the pipe 109, so that the safety is high. The shell 112 does not need to be a high-pressure container and can be reduced in weight by reducing the thickness of the container, so that the metal resources used can be reduced.

  Further, since heating can be performed in the reformer 103 by the flow of the heat medium oil 113 and natural circulation, a circulation device such as a circulation pump of the heat medium oil 113 is not necessary, and the apparatus is simplified and safety is improved. Improvements can be made.

  Further, in the raw material supply system 704, the fuel preheater 723 that requires a heat source, the raw material water evaporator 725, and the mixing unit 726 are housed in the heat medium oil storage tank 727 and immersed in the heat medium oil 113. Thus, since it heats collectively with the heating steam extracted from the water-vapor production utilization plant | facility 101, the further thermal efficiency improvement is possible.

  FIG. 12 is a configuration diagram showing a schematic configuration of the hydrogen production apparatus according to the sixth embodiment of the present invention. In this figure, the reformer 103 in FIG. 11 is replaced with the reformer 103 shown in FIG. 6, and the same or similar parts as in FIG. 6 and FIG. Omitted.

  As shown in this figure, a hydrogen production plant 102 is connected to a steam production / utilization facility 101, and steam is reformed from the fuel in the hydrogen production plant 102 to generate hydrogen using the steam thermal energy of the steam production / utilization facility 101. It is configured.

  The hydrogen production plant 102 includes a reformer 103, a raw material supply system 704 that supplies a mixed steam of fuel gas and raw material steam, and a product gas recovery system 105.

  The reformer 103 in the hydrogen production plant 102 includes a plurality of reaction tubes 411 and a shell 412 that includes the reaction tubes 411. Heat medium oil 113 is stored in the shell 412. In order to heat the heat medium oil 113, a steam pipe 414 is immersed in the heat medium oil 113.

  The reaction tube 411 constitutes a bayonet type double tube. The reaction tube 411 includes an outer tube 411A and an inner tube 411B. The outer tube 411A is fixed to the tube plate 419 with the lower end closed and the upper end opened. The inner tube 411B is open at both ends, and the upper end is fixed to the tube plate 420.

  The outer tube 411A constituting the reaction tube 411 is filled with a catalyst 115 synthesized, for example, Cu—Zn or the like. Further, as the heat medium oil 113, for example, there is a high boiling point high temperature heat medium oil such as Barrel Therm 400 (trade name), which can be used at a temperature of 300 ° C. or higher.

  The raw material supply system 704 in the hydrogen production plant 102 includes a heat medium oil storage tank 727, an attached fuel tank 722, and raw water supply system 724. The fuel tank 722 stores a fuel such as ethanol or dimethyl ether. The raw water supply system 724 includes a raw water tank that stores raw water, a feed water pump (not shown) that supplies raw water, and the like.

  The fuel stored in the fuel tank 722 is introduced into a fuel preheater 723 provided in the heat medium oil storage tank 727 and is gasified and preheated. The raw water stored in the raw water supply system 724 is supplied to a water evaporator 725 provided in the heat medium oil storage tank 727 and evaporated. The fuel gas and the raw material steam are introduced into the mixing unit 726 and become mixed steam. This mixed steam is introduced into the reformer 103 via a pipe 729.

  The medium oil storage tank 727 stores the heat medium oil 113. In the heat medium oil 113, the fuel preheater 723, the water evaporator 725, and the mixing unit 726 are immersed. A fuel heating steam pipe 728 is provided below the medium oil storage tank 727. The fuel heating steam pipe 728 is also immersed in the stored heat medium oil 113.

  In order to heat the heat medium oil 113 in the reformer 103 and the heat medium oil storage tank 727 by partially extracting the high-temperature steam produced in the steam production and use facility 101, the steam production and use facility 101 and the reformer 103 are heated. And a steam extraction pipe 109 is provided between the steam production facility 101 and the heat medium oil storage tank 727. In addition, a steam return pipe 110 for returning the heated steam to the steam production / utilization facility 101 is provided between the steam production / utilization facility 101 and the reformer 103, the steam production / utilization facility 101, the heat medium oil storage tank 727, Between the two.

  In the present embodiment, the high-temperature steam branched and extracted from the steam production / utilization facility 101 is branched and supplied to the reformer 103 and the heat medium oil storage tank 727 via the steam extraction pipe 109. The heating water vapor supplied to the heat medium oil storage tank 727 heats the heat medium oil 113 through the fuel heating steam pipe 728. The steam that has been heated is returned to the steam production / utilization facility 101 via the steam return pipe 110. In the heat medium oil storage tank 727, the heated heat medium oil 113 heats the fuel preheater 723 so that the fuel gas is heated, the water evaporator 725 is heated to generate raw material water vapor, and the mixing section At 726, the mixed gas of fuel gas and raw material steam is heated. The heated mixed gas is led to the reformer 103 and used for hydrogen reforming. At the same time, the heat medium oil 113 in the heat medium oil storage tank 727 is circulated by natural convection and heat-exchanged with the heated steam flowing in the fuel heating steam pipe 728.

  As the reformer 103, as shown in FIG. 2, a plurality of first steam pipes 114 </ b> A installed in the space region between the reaction pipes 111, and the heat medium oil 113 stored in the shell 112. The steam pipe 114 may be provided separately from the second steam pipe 114B installed in the lower layer portion. Moreover, as shown in FIG. 3, the plate fin 116 shared by the reaction tube 111 and the steam pipe 114A can also be installed.

  According to the present embodiment, the steam generated from the steam production utilization facility 101 can be used as heat energy in the reformer 103 of the hydrogen production plant 102. This steam can effectively use most of the energy required for hydrogen production, and can be used effectively without waste because it is returned to the steam production facility 101 after use. For this reason, the energy efficiency of the steam production utilization facility 101 can be further improved.

  Further, since the heating medium oil 113 is used, efficient and stable heating can be performed. In addition, high-pressure steam produced at a facility for producing and using steam is guided into the shell by piping, and the pressure boundary is piping, so the safety is high, and the shell does not need to be a high-pressure specification container. Since the thickness can be reduced and the weight can be reduced, it is possible to save resources of the metal resources to be used. Furthermore, the heat exchange efficiency is improved by heating from the outside of the catalyst packed bed by the heat medium oil 113 and heating from the inside of the packed bed of the catalyst 115 by the product gas reheated in the catalyst non-filled portion, resulting in high efficiency. Hydrogen production becomes possible.

  Further, in the raw material supply system 704, the fuel preheater 723 that requires a heat source, the raw material water evaporator 725, and the mixing unit 726 are housed in the heat medium oil storage tank 727 and immersed in the heat medium oil 113. Therefore, since it heats collectively with the heating steam extracted from the water-vapor production utilization facility 101, it becomes possible to further improve thermal efficiency.

  Further, the present invention is not limited to the embodiments described above, and the embodiments of the present invention can be implemented in combination without departing from the gist of the present invention.

The block diagram which shows schematic structure of the hydrogen production apparatus of the 1st Embodiment of this invention. The block diagram which shows schematic structure of the hydrogen production apparatus of the 2nd Embodiment of this invention. FIG. 3 is a structural diagram showing a schematic structure of a modification of the reformer of FIG. 2. FIG. 6 is a structural diagram showing a partially enlarged view of a steam pipe and its peripheral part of another modification of the reformer of FIG. 2. FIG. 9 is a structural diagram showing a partially enlarged view of a steam pipe and its peripheral portion of still another modification of the reformer of FIG. 2. The block diagram which shows schematic structure of the hydrogen production apparatus of the 3rd Embodiment of this invention. The block diagram which shows schematic structure of the hydrogen production apparatus of the 4th Embodiment of this invention. FIG. 8 is a structural diagram illustrating a schematic structure of a modification of the reformer of FIG. 7. FIG. 8 is a structural diagram showing a partially enlarged view of a steam pipe and its peripheral portion of another modification of the reformer of FIG. 7. FIG. 8 is a structural diagram showing a partially enlarged view of a steam pipe and its peripheral portion of still another modification of the reformer of FIG. 7. The block diagram which shows schematic structure of the hydrogen production apparatus of the 5th Embodiment of this invention. The block diagram which shows schematic structure of the hydrogen production apparatus of the 6th Embodiment of this invention.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 101 ... Steam production utilization facility, 102 ... Hydrogen production plant, 103 ... Reformer, 104, 704 ... Raw material supply system, 109 ... Steam extraction pipe, 110 ... Steam return pipe, 111, 411 ... Reaction pipe, 112, 412 ... Shell, 113 ... Heat transfer oil, 114, 414 ... Steam pipe, 114A ... First steam pipe, 114B ... Second steam pipe, 115 ... Catalyst, 116 ... Channel hole, 117 ... Notch channel section, 316 ... Plate fins, 317 ... Channel holes, 318 ... Notched channels, 723 ... Fuel preheater, 725 ... Raw material water evaporator, 726 ... Mixing section, 727 ... Heat medium oil storage tank, 728 ... Steam pipe for fuel heating .

Claims (10)

A raw material supply system that supplies a mixed steam containing fuel gas and raw material steam, and the mixed steam introduced from the raw material supply system is heated with steam for heating manufactured at a steam production facility to produce hydrogen by steam reforming A hydrogen generator having a reformer,
The reformer includes a plurality of reaction tubes for introducing the mixed steam, a catalyst provided in the reaction tube for steam reforming the mixed steam to promote hydrogen generation, and a shell including the reaction tube; Heat medium oil stored in the shell and in contact with at least a part of the outer surface of the reaction tube, and heating steam produced by immersion in the heat medium oil and produced in the steam production and utilization facility are introduced. And a steam pipe for heating the heat medium oil. A raw material supply system that supplies a mixed steam containing fuel gas and raw material steam, and the mixed steam introduced from the raw material supply system is heated with the steam for heating produced in the steam production and utilization facility to produce hydrogen by steam reforming. A hydrogen generator having a reformer,
The reformer includes a reaction tube that forms a double tube including a plurality of outer tubes into which the mixed steam is introduced and an inner tube that is provided in the outer tube and through which generated hydrogen flows, and the outer tube and the inner tube. And a catalyst that promotes hydrogen generation by steam reforming the mixed steam, and a shell that includes the reaction tube, and an outer surface of the outer tube that is stored in the shell. A heat medium oil that comes into contact with at least a portion of the heat medium oil, and a steam pipe that heats the heat medium oil by introducing steam for heating that is immersed in the heat medium oil and manufactured in the steam production and utilization facility. The hydrogen production apparatus characterized by the above-mentioned.   The raw material supply system includes a heat medium oil storage tank for storing the heat medium oil, a fuel preheater for preheating the fuel gas by being immersed in the heat medium oil, and heating the raw water by being immersed in the heat medium oil. The raw material water evaporator to be evaporated, a mixing part that is immersed in the heat medium oil to introduce the fuel gas and the raw material water vapor to generate mixed steam, and is immersed in the heat medium oil and manufactured at the water vapor production and utilization facility 3. A hydrogen production apparatus according to claim 1, further comprising: a fuel heating steam pipe for branching and introducing a part of the steam generated to heat the heat medium oil.   The steam pipe includes a first steam pipe installed between the plurality of reaction tubes or outer pipes, and a second steam pipe installed in a lower layer portion of the stored heat medium oil. The hydrogen production apparatus according to any one of claims 1 to 3, wherein:   2. The hydrogen production apparatus according to claim 1, further comprising plate fins for promoting heat transfer that are provided in common on the outer surfaces of the reaction tube and the steam tube.   The hydrogen production apparatus according to claim 2, further comprising a plate fin for promoting heat transfer provided in common on the outer surfaces of the outer pipe and the steam pipe.   The hydrogen production apparatus according to claim 4, further comprising a plate fin for promoting heat transfer provided in common on the outer surface of the reaction tube or the outer tube and the first steam tube.   The hydrogen production apparatus according to any one of claims 5 to 7, wherein the plate fin is provided with a flow path hole or a cut-out flow path portion through which the heat medium oil flows. Steam production facility, a raw material supply system for supplying a mixed steam containing fuel gas and raw material steam, and the mixed steam introduced from the raw material supply system is heated with the steam for heating produced in the steam production utilization facility. In a hydrogen production method for producing hydrogen using a reformer that reforms to produce hydrogen,
A plurality of reaction tubes for introducing the mixed steam, a catalyst provided in the reaction tube for steam reforming the mixed steam to promote hydrogen generation, a shell including the reaction tube, and a reservoir stored in the shell. Heat medium oil that is in contact with at least a part of the outer surface of the reaction tube and heating steam that is immersed in the heat medium oil and manufactured in the steam production and utilization facility are heated. A method for producing hydrogen, comprising producing hydrogen using the reformer comprising a steam pipe. A steam production facility, a raw material supply system for supplying a mixed steam containing fuel gas and raw material steam, and the mixed steam introduced from the raw material supply system is heated by the heating steam produced in the steam production utilization facility In a hydrogen production method for producing hydrogen using a reformer that reforms to produce hydrogen,
A reaction tube that forms a double tube including an outer tube into which the mixed vapor is introduced and an inner tube through which hydrogen generated in the outer tube flows, and an annular gap formed between the outer tube and the inner tube A catalyst that reforms the mixed steam to promote hydrogen generation by steam reforming, a shell that includes the reaction tube, and heat that is stored in the shell and is in contact with at least a part of the outer surface of the outer tube. Hydrogen using the reformer comprising: medium oil; and a steam pipe that is heated in the heat medium oil by introducing steam for heating that is immersed in the heat medium oil and manufactured in the steam production and utilization facility. A method for producing hydrogen, comprising:

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