JP5390887B2 - Hydrogen production apparatus and fuel cell system - Google Patents

Description

  The present invention relates to a hydrogen production apparatus that generates a hydrogen-rich reformed gas, and a fuel cell system including such a hydrogen production apparatus.

  A hydrogen production apparatus is known in which a raw material for hydrogen production such as kerosene or gasoline is steam reformed to produce a reformed gas, and the produced reformed gas is supplied to a fuel cell stack (see, for example, Patent Document 1). . This type of hydrogen production apparatus includes a reformer that houses a reforming catalyst. Fuel gas and water vapor are introduced into the reformer. The reforming catalyst in the reformer is heated to a predetermined temperature by a burner or the like. The steam reforming of the fuel gas and steam is promoted by the reforming catalyst heated to a predetermined temperature. The reformed gas produced by the reformer contains carbon monoxide that reduces power generation efficiency due to poisoning. Therefore, the hydrogen production apparatus is provided with a shift reaction unit that reduces carbon monoxide by an aqueous shift reaction and a selective oxidation reaction unit that further reduces carbon monoxide by a selective oxidation reaction.

JP 2004-175621 A

  However, in such a hydrogen production apparatus, it is not easy to adjust the temperature of the shift reaction unit, the temperature adjustment capability in the hydrogen production apparatus is low, and the stable operability must be low.

  An object of the present invention is to provide a hydrogen production apparatus capable of improving temperature control ability and improving stable operability, and a fuel cell system including the same.

  The hydrogen production apparatus according to the present invention removes carbon monoxide contained in the reformed gas from the reforming reaction section by reforming the liquid fuel and generating the reformed gas by the aqueous shift reaction. It is characterized by comprising a shift reaction section, and a heat exchange section that is arranged between the reforming reaction section and the shift reaction section and adjusts the temperature of the reformed gas from the reforming reaction section.

  In the hydrogen production apparatus according to the present invention, a heat exchange unit for adjusting the temperature of the reformed gas from the reforming reaction unit is disposed between the reforming reaction unit and the shift reaction unit. For this reason, the temperature of a shift reaction part will be adjusted and the temperature control capability in a hydrogen production apparatus will improve. As a result, the stable operability of the hydrogen production apparatus can be improved.

  Preferably, the heat exchange unit exchanges heat between the reformed gas from the reforming reaction unit and the exhaust heat recovery water. In this case, excessive temperature rise in the shift reaction unit can be prevented, and heat radiation from the hydrogen production apparatus can be reduced. Moreover, exhaust heat recovery efficiency can also be improved.

  Preferably, a temperature measuring unit that measures the temperature of the shift reaction unit, and an adjusting unit that adjusts the amount of exhaust heat recovery water that is heat-exchanged in the heat exchange unit based on the temperature measured by the temperature measuring unit. In addition. In this case, the degree of heat exchange in the heat exchange unit is adjusted according to the temperature of the shift reaction unit, and the temperature of the shift reaction unit can be more appropriately adjusted.

  Preferably, the adjusting means includes an on-off valve provided in the exhaust heat recovery water branch line branched from the exhaust heat recovery water line and connected to the heat exchange unit, and a temperature measured by the temperature measurement means is lower than a predetermined temperature. A control unit that controls to close the on-off valve when the temperature is low, and controls to open the on-off valve when the temperature measured by the temperature measuring means is equal to or higher than a predetermined temperature. In this case, it can prevent that the temperature of a shift reaction part rises too much.

  A fuel cell system according to the present invention includes the hydrogen production apparatus, and a fuel cell stack that generates power using a reformed gas from which carbon monoxide has been removed at least by a shift reaction unit. .

  Since the fuel cell system according to the present invention includes the hydrogen production apparatus, it is possible to improve the temperature adjustment capability of the fuel cell system and improve the stable operability of the fuel cell system.

  ADVANTAGE OF THE INVENTION According to this invention, the temperature control capability can be improved and the hydrogen production apparatus which can aim at the improvement of a stable driving | operation property, and a fuel cell system provided with the same can be provided.

It is a schematic structure figure of one embodiment of a fuel cell system concerning this embodiment. It is a flowchart which shows the control action of the electromagnetic valve provided in the waste heat recovery water branch line.

  Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the description, the same reference numerals are used for the same elements or elements having the same function, and redundant description is omitted.

  FIG. 1 is a schematic configuration diagram of an embodiment of a fuel cell system according to the present embodiment. The fuel cell system according to the present embodiment generates power using liquid fuel or gas fuel as raw fuel, and is employed as, for example, a household power supply source. Here, kerosene, which is a liquid fuel, is used from the viewpoint that it is easily available and can be stored independently.

  As shown in FIG. 1, a fuel cell system 1 includes a fuel processing system (FPS) 2 as a hydrogen production apparatus, a polymer electrolyte fuel cell (hereinafter referred to as “PEFC”) stack 3 as a fuel cell, and an inverter. 4 is provided.

  The fuel processing system 2 includes a desulfurizer 5, a reforming reaction unit 6, and a shift reaction unit 7. The desulfurizer 5 desulfurizes the introduced liquid fuel. The desulfurizer 5 is provided with a desulfurization catalyst and a heater. The desulfurization catalyst is heated to, for example, 220 ° C. to 230 ° C. by a heater and used for desulfurization. A flow path upstream of the desulfurizer 5 is provided with a pump 9 that feeds liquid fuel from the fuel tank 8 to the desulfurizer 5. The pump 9 can be fed into the desulfurizer 5 while pressurizing liquid fuel. For example, a constant flow type electromagnetic pump can be used. By pressurizing the liquid fuel in the desulfurizer 5, the liquid fuel is hardly vaporized even if the desulfurization catalyst is at a relatively high temperature. For this reason, the liquid fuel can be brought into contact with the heated desulfurization catalyst while being stably kept in a liquid state. By using a constant flow type electromagnetic pump, the pressure of the liquid fuel fed into the desulfurizer 5 can be stabilized, so that desulfurization can be performed stably.

  The liquid fuel desulfurized by the desulfurizer 5 is supplied to the reforming reaction unit 6 through the liquid fuel line L1. The reforming reaction section 6 is for reforming the liquid fuel supplied from the desulfurizer 5 to generate reformed gas, and has a reformer and a burner combustor (both not shown). doing. The reformer causes a steam reforming reaction between the desulfurized liquid fuel and steam to generate steam reformed gas containing hydrogen.

  The reformer has a vaporizer for vaporizing the desulfurized liquid fuel and raw material water, and a reforming catalyst. A liquid fuel line L1 and a reforming water line L2 for introducing water (raw water) used for steam reforming from the water tank 10 to the reformer are connected to the vaporizer of the reformer. A pump 11 that feeds water from the water tank 10 is provided in the reformed water line L2.

  The vaporized raw fuel gas and steam flow while contacting the reforming catalyst, whereby the steam reforming reaction proceeds and steam reformed gas is produced. Examples of the reforming catalyst include a catalyst in which a metal such as nickel, ruthenium, or rhodium is supported on a support made of alumina, zirconia, or the like. The steam reforming reaction is a very large endothermic reaction, and since the reaction temperature is relatively high at about 550 to 750 ° C., the reforming catalyst is heated by a burner combustor so as to be about 700 ° C. The burner combustor burns off gas or the like that is a surplus of reformed gas discharged without being used in the PEFC stack 3.

  The steam reformed gas generated in the reforming reaction unit 6 (reformer) is supplied to the shift reaction unit 7 through the reformed gas line L3. The shift reaction unit 7 performs an aqueous shift reaction of the steam reformed gas supplied from the reforming reaction unit 6 to generate a reformed gas used in a power generation reaction in which the concentration of carbon monoxide is reduced. Yes, with a shift catalyst (not shown). By using the shift reaction unit 7, a reformed gas having a carbon monoxide concentration of 1000 ppm or less is generated. Examples of the shift catalyst include a catalyst in which Cu, Zn, Fe, Cr or the like is supported on a carrier made of alumina, zirconia, or the like. The temperature range in which the aqueous shift reaction by the shift catalyst is activated is approximately 200 to 500 ° C., although it varies depending on the type of catalyst.

  A shift water line L4 for introducing shift water (raw water) used for the aqueous shift reaction from the water tank 10 to the shift reaction unit 7 is connected to the reformed gas line L3. That is, the shift water line L <b> 4 is connected between the reforming reaction unit 6 and the shift reaction unit 7. The shift water line L4 is provided with a pump 12 that sends water from the water tank 10 and a temperature raising unit 13 that raises the temperature of the shift water. The temperature raising unit 13 raises the temperature of the shift water flowing through the shift water line L4 using at least one of the desulfurizer 5 and the reforming reaction unit 6 as a heat source. That is, the shift water heated by the temperature raising unit 13 is supplied to the shift reaction unit 7.

  The reformed gas line L3 is provided with a heat exchange unit 14 that adjusts the temperature of the reformed gas from the reforming reaction unit 6. The heat exchange unit 14 exchanges heat between the steam reformed gas flowing through the reformed gas line L3 and the exhaust heat recovery water flowing through the exhaust heat recovery water branch line L6 branched from the exhaust heat recovery water line L5. Both ends of the exhaust heat recovery water line L5 are connected to the hot water storage tank 15. The exhaust heat recovery water in the hot water storage tank 15 is supplied to the exhaust heat recovery water line L5 by driving a pump (not shown), and exhaust heat recovery is performed by heat exchange at a plurality of heat exchange units including the heat exchange unit 14. As a result, it is heated and returned to the hot water storage tank 15 to heat the hot water in the hot water storage tank 15. The heat exchange unit other than the heat exchange unit 14 includes a heat exchange unit that exchanges heat between the anode off-gas and the exhaust heat recovery water, a heat exchange unit that exchanges heat between the cathode off gas and the exhaust heat recovery water, and A heat exchanging unit for exchanging heat between the flue gas from the burner combustor of the reforming reaction unit 6 and the exhaust heat recovery water is provided.

  The exhaust heat recovery water branch line L6 is provided with an electromagnetic valve 16 (open / close valve) that adjusts the amount of exhaust heat recovery water flowing through the exhaust heat recovery water branch line L6. The operation of the electromagnetic valve 16 is controlled by the control unit 17. The control unit 17 controls the operation of the electromagnetic valve 16 based on the temperature measured by a thermometer 18 (temperature measuring means) provided in the shift reaction unit 7 and measuring the temperature of the shift reaction unit 7.

  Here, the control of the electromagnetic valve 16 by the control unit 17 will be described. FIG. 2 is a flowchart showing a control operation of an electromagnetic valve provided in the exhaust heat recovery water branch line.

  As shown in FIG. 2, when the control of the electromagnetic valve 16 is started, it is determined whether or not the temperature of the shift reaction unit 7 measured by the thermometer 18 is equal to or higher than “A” (S101). The threshold “A” can be set to, for example, about 450 ° C. in consideration of the temperature range in which the aqueous shift reaction by the shift catalyst is activated.

  When determining that the temperature of the shift reaction unit 7 is not equal to or higher than “A” in step S101, the control unit 17 controls the electromagnetic valve 16 to be closed (S103), and returns to the determination in step S101. As a result, the flow of the exhaust heat recovery water toward the heat exchange unit 14 through the exhaust heat recovery water branch line L6 is blocked, and heat exchange between the steam reformed gas and the exhaust heat recovery water in the heat exchange unit 14 is performed. I will not. Therefore, the steam reformed gas is supplied to the shift reaction unit 7 without being lowered in temperature by the heat exchange unit 14, and the aqueous shift reaction in the shift reaction unit 7 is promoted.

  On the other hand, if the control unit 17 determines in step S101 that the temperature of the shift reaction unit 7 is equal to or higher than “A”, the control unit 17 controls to open the electromagnetic valve 16 (S105), and returns to the determination in step S101. Thereby, the exhaust heat recovery water is supplied to the heat exchange unit 14 through the exhaust heat recovery water branch line L6, and heat exchange between the steam reformed gas and the exhaust heat recovery water in the heat exchange unit 14 is performed. Therefore, the steam reformed gas is supplied to the shift reaction unit 7 after the temperature is lowered in the heat exchange unit 14, and the aqueous shift reaction in the shift reaction unit 7 is suppressed. As a result, it is possible to prevent the temperature of the shift reaction unit 7 from rising excessively.

  Reference is again made to FIG. The PEFC stack 3 is configured by stacking a plurality of battery cells (not shown), and generates power using the hydrogen-rich reformed gas obtained by the fuel processing system 2 to output a DC current. The battery cell has an anode, a cathode, and an electrolyte that is a solid oxide disposed between the anode and the cathode. By introducing the reformed gas into the anode and introducing air into the cathode, An electrochemical power generation reaction is performed in each battery cell. The PEFC stack 3 normally operates at a temperature of about 70 ° C.

  The inverter 4 converts the output DC current into AC current. The desulfurizer 5, the fuel processing system 2 (the reforming reaction unit 6 and the shift reaction unit 7), the PEFC stack 3, and the inverter 4 are accommodated in a housing (not shown) and modularized.

  As described above, in this embodiment, the heat exchange unit 14 that adjusts the temperature of the reformed gas from the reforming reaction unit 6 is disposed between the reforming reaction unit 6 and the shift reaction unit 7. For this reason, the temperature of the shift reaction unit 7 is adjusted, and the temperature adjustment capability in the fuel processing system 2 is improved. As a result, the stable operability of the fuel processing system 2 can be improved.

  In the present embodiment, the heat exchange unit 14 exchanges heat between the reformed gas from the reforming reaction unit 6 and the exhaust heat recovery water flowing through the exhaust heat recovery water branch line L6. For this reason, the excessive temperature rise of the shift reaction part 7 can be prevented, and the heat radiation from the fuel processing system 2 can be reduced. In addition, the exhaust heat recovery efficiency in the fuel cell system 1 can be improved.

  In the present embodiment, a thermometer 18 that measures the temperature of the shift reaction unit 7 and an electromagnetic that adjusts the amount of exhaust heat recovery water that is heat-exchanged in the heat exchange unit 14 based on the temperature measured by the thermometer 18. A valve 16 and a controller 17 that controls the operation of the electromagnetic valve 16 are provided. For this reason, according to the temperature of the shift reaction part 7, the heat exchange degree in the heat exchange part 14 will be adjusted, and the temperature of the shift reaction part 7 can be adjusted much more appropriately.

  In the present embodiment, the control unit 17 controls the electromagnetic valve 16 to be closed when the temperature measured by the thermometer 18 is lower than the predetermined temperature, and when the temperature measured by the thermometer 18 is equal to or higher than the predetermined temperature. The electromagnetic valve 16 is controlled to open. For this reason, it can prevent reliably that the temperature of the shift reaction part 7 rises excessively.

  The preferred embodiments of the present invention have been described above. However, the present invention is not necessarily limited to the above-described embodiments, and various modifications can be made without departing from the scope of the present invention.

  For example, the PEFC stack 3 is not limited to a solid polymer fuel cell stack, and may be a solid oxide fuel cell stack or the like.

  For example, the reformer of the reforming reaction unit 6 is not limited to one that performs steam reforming, and may be one that undergoes partial oxidation reforming or autothermal reforming. The reforming method using the reformer is based on characteristics of liquid fuel such as kerosene, gasoline, naphtha, light oil, methanol, ethanol, DME (dimethyl ether), biofuel using biomass, and the like.

  The control unit 17 controls the opening and closing of the electromagnetic valve 16 based on the temperature measured by the thermometer 18, but is not limited thereto, and the opening of the electromagnetic valve 16 is performed based on the temperature measured by the thermometer 18. The degree may be controlled.

  In the present embodiment, the shift reaction unit 7 reduces the concentration of carbon monoxide in the reformed gas sent from the reforming reaction unit 6, but the present invention is not limited to this. A selective oxidation reaction unit that further reduces carbon monoxide by a selective oxidation reaction is provided at the subsequent stage of the shift reaction unit 7, and one of the reformed gases sent from the reforming reaction unit 6 by the shift reaction unit 7 and the selective oxidation reaction unit. The concentration of carbon oxide may be reduced.

DESCRIPTION OF SYMBOLS 1 ... Fuel cell system, 2 ... Fuel processing system, 6 ... Reformation reaction part, 7 ... Shift reaction part, 14 ... Heat exchange part, 16 ... Electromagnetic valve, 17 ... Control part, 18 ... Thermometer, L3 ... Reformation Gas line, L5 ... Waste heat recovery water line, L6 ... Waste heat recovery water branch line.

Claims (4)

A reforming reaction section for reforming liquid fuel to generate reformed gas;
A shift reaction section for removing carbon monoxide contained in the reformed gas from the reforming reaction section by an aqueous shift reaction;
A heat exchange part that is arranged between the reforming reaction part and the shift reaction part and adjusts the temperature of the reformed gas from the reforming reaction part,
The heat exchange unit recovers the reformed gas from the reforming reaction unit and the exhaust heat recovery branching from the exhaust heat recovery line connected to the hot water tank and flowing through the exhaust heat recovery branch line connected to the heat exchange unit Exhaust heat recovery water that exchanges heat with water and flows through the exhaust heat recovery branch line is heat-exchanged only with the heat exchange unit. Temperature measuring means for measuring the temperature of the shift reaction section;
2. The apparatus according to claim 1, further comprising an adjusting unit that adjusts an amount of exhaust heat recovery water that is heat-exchanged in the heat exchange unit based on a temperature measured by the temperature measuring unit. Hydrogen production equipment. The adjusting means is
An opening and closing valve provided in the exhaust heat recovery water branch line,
Control to close the on-off valve when the temperature measured by the temperature measuring means is lower than a predetermined temperature, and control to open the on-off valve when the temperature measured by the temperature measuring means is equal to or higher than a predetermined temperature. The hydrogen production apparatus according to claim 2, further comprising: The hydrogen production apparatus according to any one of claims 1 to 3,
A fuel cell system, comprising: a fuel cell stack that generates power using at least the reformed gas from which carbon monoxide has been removed by the shift reaction unit.

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