JP2006290663A - Reformed gas utilization system - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a reformed gas utilization system allowing stable operation of a reformed gas utilization apparatus. <P>SOLUTION: Heat is transferred in a heat exchanger 30 between a reformed gas reformed and generated in a PSR-type reformer 10 or a PSR-type reformer 20 and an anode off-gas exhausted from a hydrogen separation membrane-type fuel cell 40, and the temperature of the reformed gas is adjusted approximately to the operation temperature of the hydrogen separation membrane-type fuel cell 40, before the reformed gas is supplied to the hydrogen separation membrane-type fuel cell 40. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a reformed gas utilization system, and more particularly, to a reformed gas utilization system provided with a reforming reaction apparatus that switches between a fuel reforming reaction using a catalyst and a regeneration reaction (exothermic reaction) for heating and regenerating the catalyst.

  A reforming reaction device that reforms a reforming fuel such as fossil fuel to generate a reformed gas (hydrogen-rich gas), a reformed gas utilization device that operates using the obtained reformed gas, As a reformed gas utilization system equipped with a catalyst, for example, a plurality of modifications are performed by switching between a steam reforming reaction of fuel that is an endothermic reaction using a catalyst and an exothermic reaction that regenerates the catalyst temperature decreased by the steam reforming reaction. A fuel cell system having a reforming reaction apparatus equipped with a quality reactor has been proposed (see, for example, Patent Document 1). In addition to the above, there are technologies disclosed as related technologies (for example, see Patent Documents 2 to 4).

In the reforming reaction apparatus described in Patent Document 1, one of the two reforming reactors is subjected to a steam reforming reaction which is an endothermic reaction using heat storage in the reactor, and the other is caused to perform an exothermic reaction. When the one heat storage amount is reduced by the steam reforming reaction, the heat conversion is switched to the exothermic reaction, and the other is switched to the reforming reaction so that the fuel reforming is performed by the heat stored by the exothermic reaction. This eliminates the need for a separate heater and enables continuous hydrogen generation with high use efficiency of heat energy.
U.S. Patent No. 2004-175326 U.S. Patent No. 2004-170558 US Patent No. 2004-170559 US 2003-235529

  Since the steam reforming reaction, which is an endothermic reaction, occurs using heat stored in the reforming reactor due to an exothermic reaction, the temperature of the reformed gas decreases as the steam reforming reaction proceeds. For this reason, the temperature of the reformed gas supplied to the reformed gas utilization device such as a fuel cell cannot be kept constant, which may hinder the stable operation of the reformed gas utilization device.

  The present invention has been made in view of the above problems, and an object of the present invention is to provide a reformed gas utilization system that enables stable operation of the reformed gas utilization apparatus.

  The reformed gas utilization system of the present invention for achieving the above object includes a catalyst, and when the reforming raw material is supplied, the reforming raw material is reformed on the heated catalyst to generate heat. When a fuel is supplied, a reforming reactor having at least two reforming reactors for heating the catalyst by causing an exothermic reaction of the exothermic fuel and a reformed gas generated by the reforming reactor are supplied. The reformed gas utilization device that operates in this manner, and temperature adjusting means that brings the temperature of the reformed gas close to the operating temperature of the reformed gas utilization device.

  The reforming reaction apparatus according to the reformed gas utilization system of the present invention switches between a steam reforming reaction of fuel that uses heat storage and an exothermic reaction that recovers the heat storage amount (that is, the catalyst temperature) that has decreased due to the steam reforming reaction. At least two reforming reactors (hereinafter also referred to as “PSR (Pressure swing reforming) type reformers”) that can be performed, and at least one reforming reaction of the fuel, An exothermic reaction is performed in at least one other unit (hereinafter, the reforming reaction apparatus may be referred to as “PSR reforming apparatus”).

  For example, when there are two reforming reactors, one of them is subjected to a steam reforming reaction using heat storage in the reactor and the other is caused to perform an exothermic reaction, and the one heat storage amount is caused by the steam reforming reaction. When it decreases, the reaction is switched to an exothermic reaction, and the other is switched to a reforming reaction so that the fuel reforming is performed with the heat stored by the exothermic reaction.

  The temperature of the reformed gas generated by the steam reforming reaction is substantially the same as the outlet temperature of the catalyst provided in the reforming reactor. When the steam reforming reaction proceeds in one reforming reactor, the catalyst temperature Gradually decreases, and the temperature of the reformed gas also decreases accordingly. Further, when the steam reforming reaction is performed in the other reforming reactor, the temperature of the reformed gas rises because the catalyst temperature of the other reforming reactor is high (the amount of stored heat is large). Therefore, the temperature of the reformed gas supplied from the PSR reformer is not constant.

  The reformed gas utilization system of the present invention includes a temperature adjusting means for bringing the temperature of the reformed gas supplied from the PSR reformer closer to the operating temperature of the reformed gas utilization device, thereby realizing stable operation of the reformed gas utilization device. it can.

  In the present invention, a mixed gas of reforming fuel and water vapor is used as the reforming raw material. Among reforming fuels, hydrocarbon fuels (eg, methane gas, gasoline, etc.) that are commonly used as fuels for obtaining hydrogen and carbon monoxide synthesis gas (hydrogen-containing gas) through reforming reactions such as steam reforming. Can be appropriately selected and used. In addition to the hydrocarbon fuel described above, a reformed gas generated by a reforming reaction or the like can be used as the heat generating fuel used in the present invention.

  In the reformed gas utilization system of the present invention, the temperature adjusting means may be a heat exchanger that transfers heat between the exhaust gas discharged from the reformed gas utilization device and the reformed gas. preferable. By using the heat exchanger, the temperature of the reformed gas can be brought close to the operating temperature of the reformed gas utilization apparatus without separately providing a heating means for heating the reformed gas and a cooling means for cooling. Therefore, the system can be simplified.

  The reformed gas utilization device may be a fuel cell. There are various types of fuel cells, such as solid polymer type and solid oxide type. Depending on the type, there is an optimum operating temperature, and if the operating temperature is low, the proton conductivity of the electrolyte membrane decreases, so power generation efficiency However, when the operating temperature is high, the deterioration of the fuel cell may be promoted. Since the reformed gas utilization system of the present invention includes temperature adjusting means for bringing the temperature of the reformed gas close to the operating temperature of the fuel cell that is the reformed gas utilization apparatus, the variation of the operating temperature of the fuel cell due to the variation of the reformed gas temperature And stable operation of the fuel cell can be realized.

  The fuel cell used in the present invention is not particularly limited, but a fuel cell that operates near the temperature (300 to 600 ° C.) of the reformed gas supplied from the PSR reformer is preferable, and the hydrogen permeable metal layer A fuel cell provided with an electrolyte in which an electrolyte layer is laminated on at least one side of is effective.

  ADVANTAGE OF THE INVENTION According to this invention, the reformed gas utilization system which enables the stable operation | movement of a reformed gas utilization apparatus can be provided.

  Hereinafter, embodiments of the reformed gas utilization system of the present invention will be described in detail with reference to the drawings. In the present embodiment, a case where combustion fuel is used as an example of the heat generating fuel will be described.

  The reformed gas utilization system of the present invention uses a mixed gas of gasoline and steam as a reforming raw material to be supplied to the reforming reaction apparatus, and proton reforming the membrane surface of the hydrogen permeable metal film as the reformed gas utilization apparatus. Using a Hydrogen Separation Membrane Fuel Cell (HMFC) with a Laminate Ceramic Laminate as an Electrolyte Membrane, and Reforming Produced by Hydrogen Separation Membrane Fuel Cell Anode Offgas and Reforming Reactor as Temperature Control Means The heat exchanger is configured to exchange heat with gas.

  FIG. 1 is a schematic configuration diagram showing an example of an embodiment of a reformed gas utilization system of the present invention. The reformed gas utilization system according to the present embodiment includes a first PSR reformer 10 and a second PSR reformer 10 that are provided with a catalyst and can switch between a reforming reaction and an exothermic reaction (combustion reaction). A reforming reaction apparatus having a PSR reformer 20, a heat exchanger 30, and a hydrogen separation membrane fuel cell 40 are provided.

  The PSR type reformer 10 and the PSR type reformer 20 are configured by a cylindrical body having a circular cross section whose both ends are closed, and a catalyst (catalyst supporting portion) supported on the inner wall surface of the cylindrical body. The cylindrical body forms a space for performing the reaction and a gas flow path, and also functions as a catalyst carrier.

  The cylindrical body is a hollow body that is formed into a cylindrical shape having a circular cross section with a diameter of 10 cm using a ceramic honeycomb, and both ends in the length direction of the cylinder are closed. As the cross-sectional shape and size, an arbitrary shape and size such as a rectangle other than a circle and an ellipse can be selected according to the purpose and the like.

  The catalyst does not carry a catalyst on the curved surface of the cylindrical body wall in the vicinity of the center of the cylinder from the both ends of the cylindrical body in the longitudinal direction, that is, at a predetermined distance from both ends in the longitudinal direction. It is left as a catalyst non-supporting part and is supported on the entire surface excluding the catalyst non-supporting part. As the catalyst, metals such as Pd, Ni, Pt, Rh, Ag, Ce, Cu, La, Mo, Mg, Sn, Ti, Y, and Zn can be used.

As shown in FIG. 2, the hydrogen separation membrane fuel cell 40 includes an electrolyte membrane 51 having a dense hydrogen permeable layer using a hydrogen permeable metal, and an oxygen electrode (O ₂ electrode) 52 sandwiching the electrolyte membrane 51. And a hydrogen electrode (H ₂ electrode) 53. When the reformed gas is supplied, hydrogen can be selectively permeated to perform power generation operation.

  Between the oxygen electrode 52 and the electrolyte membrane 51, an air flow path 59 a for passing, that is, supplying and discharging air (Air) as an oxidant gas is formed, and between the hydrogen electrode 53 and the electrolyte membrane 51. A fuel flow path 59b for passing, that is, supplying and discharging hydrogen-rich fuel gas (in this case, reformed gas generated by reforming) is formed. The oxygen electrode 52 and the hydrogen electrode 53 are made of various materials such as carbon (for example, carbon powder carrying platinum or an alloy composed of platinum and other metals) or an electrolyte solution (for example, Nafion Solution manufactured by Aldrich Chemical). Can be formed.

The electrolyte membrane 51 has a four-layer structure including a dense substrate (dense hydrogen permeable layer made of a hydrogen permeable metal) 56 formed of vanadium (V). The palladium (Pd) layers (dense hydrogen permeable layers made of a hydrogen permeable material) 55 and 57 are provided so as to sandwich the base material 56 from both sides, and are opposite to the side of the one Pd layer 55 in contact with the base material 56. On the side surface, an electrolyte layer 54 made of BaCeO ₃ (solid oxide) is further provided in a thin layer shape.

  The base material 56 can be suitably formed using niobium, tantalum, and an alloy containing at least one of these in addition to vanadium (V). These have high hydrogen permeability and are relatively inexpensive.

Electrolyte layer (BaCeO ₃ layer) 54 can be configured by using a SrCeO ₃ based ceramic proton conductor other than BaCeO _3.

  Examples of the hydrogen permeable metal include, in addition to palladium, vanadium, niobium, tantalum, an alloy containing at least one of these, and a palladium alloy. The electrolyte layer can be protected by providing a dense layer using these.

  The dense layer (coating) made of a hydrogen permeable metal generally contains, for example, vanadium (vanadium alone and an alloy such as vanadium-nickel) on the oxygen electrode side because it is generally highly hydrogen permeable and relatively inexpensive. ), Niobium, tantalum, and alloys containing at least one of these are preferably used. Although these can be applied on the hydrogen electrode side, the oxygen electrode side is desirable in terms of avoiding hydrogen embrittlement. On the hydrogen electrode side, it is preferable to use, for example, palladium or a palladium alloy because hydrogen permeability is relatively high and hydrogen embrittlement is difficult.

  As shown in FIG. 2, it has a sandwich structure consisting of three layers of Pd layer 55 / base material 56 / Pd layer 57, that is, a laminated structure of two or more layers made of different metals (dense layers made of hydrogen permeable material). In this case, a metal diffusion suppression layer that suppresses diffusion of the different metals may be provided on at least a part of the contact interface of the different metals (see, for example, FIGS. 4 and 5). The metal diffusion suppressing layer is described in paragraphs [0015] to [0016] of JP-A No. 2004-146337.

  As described above, the sandwich structure may be provided as a five-layer structure such as Pd / tantalum (Ta) / V / Ta / Pd in addition to palladium (Pd) / vanadium (V) / Pd. V has a faster proton or hydrogen atom permeation rate than Pd and is inexpensive, but has a low ability to dissociate hydrogen molecules into protons, etc., so a Pd layer having a high ability to protonate hydrogen molecules is attached to one or both sides of the V layer. By providing it on the surface, the transmission performance can be improved. In this case, by providing a metal diffusion suppressing layer between the metal layers, mutual diffusion between different metals can be suppressed, and a decrease in hydrogen permeation performance and hence a decrease in electromotive force of the fuel cell can be suppressed.

  The electrolyte layer 54 is made of a solid oxide, and a reaction suppression layer that suppresses the reaction between oxygen atoms in the electrolyte layer and Pd may be provided at least at a part of the interface with the Pd layer 55 ( For example, the reaction suppression layer 65 in FIG. This reaction suppression layer is described in paragraphs [0024] to [0025] of JP-A No. 2004-146337.

  The electrolyte membrane 51 includes a vanadium base material, which is a dense hydrogen permeable material, and an inorganic electrolyte layer formed on the cathode side of the fuel cell, so that the electrolyte layer can be made thin. The operating temperature of the high-temperature type solid oxide fuel cell (SOFC) can be lowered to a temperature range of 300 to 600 ° C.

In the hydrogen separation membrane fuel cell 40, when a reformed gas having a high hydrogen (H ₂ ) density is supplied to the fuel flow path 59b and air containing oxygen (O ₂ ) is supplied to the air flow path 59a, the following formula is obtained. The electrochemical reaction (battery reaction) represented by (1) to (3) is caused and electric power is supplied to the outside. Equations (1) and (2) represent reactions on the anode side and cathode side, respectively, and equation (3) represents the total reaction in the fuel cell.

H ₂ → 2H ⁺ + 2e ⁻ (1)
(1/2) O ₂ + 2H ⁺ + 2e ⁻ → H ₂ O (2)
H ₂ + (1/2) O ₂ → H ₂ O (3)

  A pipe 102 for supplying a reforming raw material is connected to one end of the PSR reformer 10 and one end of the PSR reformer 20 via a valve V1 and a valve V3. By controlling the opening and closing of the valve V1 and the valve V3, the reforming raw material is supplied to the PSR reformer 10 or the PSR reformer 20, and the reforming reaction is started. The other end of the PSR reformer 10 and the PSR reformer 20 is connected to a pipe 104 via a valve V5 and a valve V7 so that the reformed gas generated in the reforming reactor can be taken out. Are connected at one end. The other end of the pipe 104 is connected to the heat exchanger 30. One end of the pipe 106 is connected to the heat exchanger 30, and the other end is connected to the reformed gas supply port of the fuel flow path 59 b of the hydrogen separation membrane fuel cell 40. The piping 104 and the piping 106 are communicated with each other via the heat exchanger 30, and the reformed gas generated by the PSR reformer 10 or the PSR reformer 20 is supplied to the hydrogen separation membrane fuel cell 40. It has become so.

  One end of the pipe 108 is connected to the anode offgas discharge port of the fuel flow path 59 b of the hydrogen separation membrane fuel cell 40, and the other end of the pipe 108 is connected to the heat exchanger 30. One end of the pipe 110 is connected to the heat exchanger 30, and the other end of the pipe 110 is connected to the PSR reformer 10 and the PSR reformer 20 via the valve V6 and the valve V8. The pipe 108 and the pipe 110 are communicated with each other via the heat exchanger 30, and the PSR reformer is controlled by controlling the opening and closing of the valve V6 and the valve V8 of the anode off-gas discharged from the hydrogen separation membrane fuel cell 40. 10 or PSR reformer 20 can be supplied. Hydrogen gas that did not contribute to the cell reaction remains in the anode off gas, and this hydrogen gas can be used as a combustion fuel. Further, the PSR reformer 10 and the PSR reformer 20 are supplied with air from a supply means (not shown) via a pipe 110, and the combustion fuel and oxygen in the air are supplied. The reaction causes a combustion reaction.

  A pipe 112 for supplying air, which is an oxidant gas, is connected to the air supply port of the air flow path 59a of the hydrogen separation membrane fuel cell 40, and the cathode off gas is discharged to the cathode off gas discharge port of the air flow path 59a. A pipe 114 is connected as possible.

  By performing heat transfer between the reformed gas and the anode off gas in the heat exchanger 30, the temperature of the reformed gas can be adjusted to be close to the temperature of the anode off gas. The exhaust gas from the hydrogen separation membrane fuel cell 40 includes, in addition to the anode off gas, a cathode off gas or a cooling medium that has passed through a cooling passage (not shown) for cooling the hydrogen separation membrane fuel cell 40, and the reformed gas. Although heat transfer may be performed between the cathode offgas and the cooling medium, it is preferable that heat transfer be performed between the anode offgas and the reformed gas that are substantially equal to the operating temperature of the fuel cell.

  On the side where the pipes 102 of the PSR reformer 10 and the PSR reformer 20 are connected, a pipe 116 is connected via valves V2 and V4 so that off-gas from the reforming reactor can be discharged. Has been.

  Next, the operation of the reformed gas utilization system of the present invention will be described. First, an operation for reformed gas generation by the PSR reformer will be described. The reforming raw material is supplied to the PSR reformer 10 which has reached the steam reforming temperature with the valves V1, V4, V5 and V8 opened and the valves V2, V3, V6 and V7 closed. An anode off gas and air are supplied to the PSR reformer 20 through the pipe 110 as fuel for combustion. As a result, the PSR reformer 10 performs the steam reforming reaction using the heat storage of the reforming reactor, and the reformed gas generated by reforming is taken out through the pipe 104. Further, in the PSR reformer 20, the catalyst is heated by the combustion reaction until the reformable temperature is reached, and the combustion off gas is discharged through the pipe 116.

  When the temperature of the PSR reformer 10 decreases to a range not suitable for the steam reforming reaction as the reforming reaction proceeds, the valve V1, the valve V4, the valve V5, and the valve V8 are closed, and the valve V2, the valve V3, the valve The reforming material is supplied through the pipe 102 to the PSR reformer 20 that has reached the reformable temperature by opening the valve V6 and the valve V7, and the anode off-gas and air are supplied to the PSR reformer 10 through the pipe 110. The By repeating this switching, the reformed gas is supplied to the hydrogen separation membrane fuel cell 40.

  The reformed gas supplied to the hydrogen separation membrane fuel cell 40 through the piping 104 and the piping 106 exchanges heat with the anode off-gas discharged from the hydrogen separation membrane fuel cell 40 in the heat exchanger 30 to generate hydrogen. After being adjusted to the vicinity of the optimum operating range of the separation membrane fuel cell 40, it is supplied to the hydrogen separation membrane fuel cell 40. Also, air is supplied from the piping 112 to the hydrogen separation membrane fuel cell 40, and hydrogen in the reformed gas and oxygen in the air cause a cell reaction to supply power to the outside.

  FIG. 3 is a conceptual diagram showing the relationship between the reforming reactor switching timing and the reforming gas temperature in the vicinity of the reforming reactor outlet and in the vicinity of the reforming gas supply port of the fuel flow path 59b. When the reformed gas temperature near the reforming reactor outlet is higher than the operating temperature (anode offgas temperature) of the fuel cell, the reformed gas is removed by the heat exchanger 30 and the reformed gas near the reforming reactor outlet is removed. When the temperature is lower than the operating temperature of the fuel cell, the reformed gas is heated with a heat exchanger. Thereby, the reformed gas can be adjusted to the vicinity of the optimum operating temperature of the fuel cell. By supplying the reformed gas to the hydrogen separation membrane fuel cell 40 via the heat exchanger 30, the hydrogen separation membrane fuel cell 40 can be stably operated.

  As the reformed gas utilization apparatus according to the present invention, a hydrogen separation membrane type comprising an electrolyte membrane in which an electrolyte layer is laminated on at least one surface of a dense hydrogen permeable membrane (hydrogen permeable metal layer) using a hydrogen permeable metal. It can be selected from fuel cells (proton conductive solid oxide type or solid polymer type) according to the purpose.

  For example, (1) an electrolyte membrane having a hydrogen permeable metal and an inorganic electrolyte layer (especially proton conductive ceramics) formed on at least one side of the metal, and hydrogen provided on one surface of the electrolyte membrane A fuel supply part for supplying power generation fuel to the electrode and the hydrogen electrode, an oxygen electrode provided on the other surface of the electrolyte membrane, and an oxidant gas supply part for supplying an oxidant gas to the oxygen electrode Hydrogen separation membrane fuel cell, or (2) an electrolyte membrane having a proton conductive electrolyte layer and a hydrogen permeable metal sandwiching the electrolyte layer from both sides, a hydrogen electrode provided on one surface of the electrolyte membrane, and the A solid polymer comprising a fuel supply unit for supplying power generation fuel to the hydrogen electrode, an oxygen electrode provided on the other surface of the electrolyte membrane, and an oxidant gas supply unit for supplying an oxidant gas to the oxygen electrode Type hydrogen separation membrane fuel cell, etc. It can be used to apply.

  4 to 5 show other specific examples of the hydrogen separation membrane fuel cell constituting the reformed gas utilization system of the present invention. For details about other specific examples, reference can be made to the description in Japanese Patent Application Laid-Open No. 2004-146337.

FIG. 4 shows an electrolyte membrane 61 having a five-layer structure including a dense substrate 66 made of vanadium (V), an oxygen electrode (O ₂ electrode) 62 and a hydrogen electrode (H ₂ electrode) sandwiching the electrolyte membrane 61. ) 63 and a hydrogen separation membrane fuel cell 60 provided with a metal diffusion suppression layer and a reaction suppression layer. The electrolyte membrane 61 is provided with a dense metal diffusion suppression layer 67 and a palladium (Pd) layer 68 in this order from the surface side of the base electrode 66 on the hydrogen electrode (anode) 63 side. On the surface of the cathode 62 side, a dense reaction suppression layer (for example, a proton conductor, mixed conductor, or insulator layer) 65 and a thin electrolyte layer (for example, a perovskite layer) made of a solid oxide are sequentially formed from the surface side. One metal oxide SrCeO ₃ layer, etc.) 64. The reaction suppression layer 65 has a function of suppressing the reaction between oxygen atoms in the electrolyte layer 64 and the base material (V) 66. In the same manner as described above, an air channel 59a and a fuel channel 59b are formed between the oxygen electrode or hydrogen electrode and the electrolyte membrane. Details of the metal diffusion suppression layer and the reaction suppression layer are as described above.

FIG. 5 includes an electrolyte membrane 71 having a dense hydrogen permeable layer using a hydrogen permeable metal, and an oxygen electrode (O ₂ electrode) 72 and a hydrogen electrode (H ₂ electrode) 73 sandwiching the electrolyte membrane 71. The solid polymer type hydrogen separation membrane fuel cell 70 is shown. The electrolyte membrane 71 has, for example, a multilayer structure in which the surfaces on both sides of an electrolyte layer 76 made of a solid polymer membrane such as a Nafion (registered trademark) membrane are sandwiched between dense hydrogen permeable metal layers. A palladium (Pd) layer (dense layer) 77 is provided on the hydrogen electrode (anode) side surface of 76, and a vanadium-nickel serving as a base material in order from the surface side on the oxygen electrode (cathode) side surface of the electrolyte layer 76. An alloy (V—Ni) layer (dense layer) 75 and a Pd layer (dense layer) 74 are provided. As described above, an air channel 59a and a fuel channel 59b are formed between the oxygen electrode or hydrogen electrode and the electrolyte membrane 71, respectively. Also in the present fuel cell, a metal diffusion suppression layer can be provided between the V-Ni layer 75 and the Pd layer 74, and a reaction occurs between the V-Ni layer 75 or the Pd layer 77 and the electrolyte layer 76. A suppression layer can be provided.

  In the polymer electrolyte fuel cell shown in FIG. 5, by forming a hydrogen permeable layer using a hydrogen permeable metal so as to sandwich the water-containing electrolyte layer, moisture evaporation and membrane resistance of the electrolyte layer at a high temperature are achieved. The increase can be suppressed, and generally the operating temperature of a low-temperature polymer electrolyte fuel cell (PEFC) can be improved to a temperature range of 300 to 600 ° C.

  In the above embodiment, the case where a mixed gas of gasoline and water vapor is used as the reforming raw material has been described, but the same applies to the case where a hydrocarbon fuel other than gasoline is used. Examples of the reformed gas utilization device other than the fuel cell include a hydrogen engine, a hydrogen gas addition device for an internal combustion engine, and the like.

It is a schematic structure figure showing an example of an embodiment of a reformed gas utilization system. It is a schematic sectional drawing which shows a hydrogen separation membrane type fuel cell. It is the conceptual diagram which showed the relationship between the switching timing of a reforming reactor, and reformed gas temperature. It is a schematic sectional drawing which shows the other specific example of a hydrogen separation membrane fuel cell. It is a schematic sectional drawing which shows the other specific example of a hydrogen separation membrane fuel cell.

Explanation of symbols

10 First PSR reformer 20 Second PSR reformer 30 Heat exchanger 40 Hydrogen separation membrane fuel cell 51 Electrolyte membrane 52 Oxygen electrode 53 Hydrogen electrode 59a Air channel 59b Fuel channel

Claims (4)

When the reforming raw material is supplied, the reforming raw material is reformed on the heated catalyst, and when the exothermic fuel is supplied, the exothermic fuel is exothermicly reacted. A reforming reactor having at least two reforming reactors for heating
A reformed gas utilization device that operates by being supplied with the reformed gas generated in the reforming reaction device;
Temperature adjusting means for bringing the temperature of the reformed gas close to the operating temperature of the reformed gas utilization device;
Reformed gas utilization system equipped with.   The reformed gas utilization system according to claim 1, wherein the temperature adjusting means is a heat exchanger that exchanges heat between the exhaust gas discharged from the reformed gas utilization device and the reformed gas.   The reformed gas utilization system according to claim 1 or 2, wherein the reformed gas utilization device is a fuel cell.   The reformed gas utilization system according to claim 3, wherein the fuel cell includes an electrolyte in which an electrolyte layer is laminated on at least one surface of a hydrogen permeable metal layer.

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