WO2009139159A1 - 水素発生装置及び燃料電池発電装置 - Google Patents
水素発生装置及び燃料電池発電装置 Download PDFInfo
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- WO2009139159A1 WO2009139159A1 PCT/JP2009/002095 JP2009002095W WO2009139159A1 WO 2009139159 A1 WO2009139159 A1 WO 2009139159A1 JP 2009002095 W JP2009002095 W JP 2009002095W WO 2009139159 A1 WO2009139159 A1 WO 2009139159A1
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- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
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- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
- C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
- C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
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- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
- H01M8/0625—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material in a modular combined reactor/fuel cell structure
- H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
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- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
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- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
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- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
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- B01J2208/00008—Controlling the process
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0435—Catalytic purification
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- C01B2203/08—Methods of heating or cooling
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- C01B2203/1288—Evaporation of one or more of the different feed components
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- C01B2203/1695—Adjusting the feed of the combustion
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Definitions
- the present invention uses a hydrocarbon-based fuel such as city gas and LPG as a raw material gas to generate a product gas containing high-concentration hydrogen, and to generate power using the hydrogen generated by the hydrogen generator.
- a hydrocarbon-based fuel such as city gas and LPG
- the present invention relates to a fuel cell power generator equipped with a fuel cell.
- the fuel cell power generator is mainly composed of a hydrogen generator that generates a product gas containing high-concentration hydrogen and a fuel cell that generates power using hydrogen generated by the hydrogen generator.
- a hydrogen generator uses a hydrocarbon-based fuel such as city gas or LPG as a raw material gas, and performs a steam reforming reaction between the raw material gas and steam using a reforming catalyst, thereby producing hydrogen, methane, carbon monoxide (10 to 10%). About 15%), a reforming section that generates reformed gas containing carbon dioxide or water vapor, and a carbon monoxide removing section that removes carbon monoxide having a poisoning action on the fuel cell from the reformed gas. It is formed with.
- a hydrocarbon-based fuel such as city gas or LPG
- a reforming catalyst thereby producing hydrogen, methane, carbon monoxide (10 to 10%).
- a reforming section that generates reformed gas containing carbon dioxide or water vapor
- a carbon monoxide removing section that removes carbon monoxide having a poisoning action on the fuel cell from the reformed gas. It is formed with.
- the carbon monoxide removal unit is a selective oxidation reaction by mixing with oxygen using a selective oxidation catalyst by removing the carbon monoxide to about 0.5% by a shift reaction using a modification catalyst.
- it is formed of a two-stage constituent part including a selective oxidation part that oxidizes carbon monoxide to reduce the CO concentration to about 10 ppm or less.
- the raw material supply amount and the water supply amount are changed to increase or decrease the amount of hydrogen produced.
- the water evaporation part is balanced to a temperature that can be evaporated by heat from the combustion exhaust gas from the burner surrounding the surroundings or from the catalyst layer. However, if a large amount of water is suddenly shared, depending on the situation, the supplied water may not be completely evaporated and may be supplied to the reforming catalyst in the state of partially unvaporized droplets.
- the temperature of the reforming catalyst rapidly decreases locally because the latent heat when the droplets evaporate is taken away from the reforming catalyst.
- the temperature of the surrounding catalyst is also lowered, so that the reforming catalyst as a whole cannot maintain a stable temperature state, and there is a possibility that the generation amount of hydrogen is disturbed.
- the second evaporation unit is installed at the lower part of the downstream part of the water evaporation unit, and the partition is provided at the lower part and the side surface of the second evaporation unit. Only the water vapor trapped in the lower part of the second evaporation unit and evaporated after being trapped is sent out from the second evaporation unit (see, for example, Patent Document 1).
- the increase in the number of parts and the complexity of the structural configuration may increase the parts and manufacturing costs.
- the size of the entire hydrogen generation device increases, and the surface area of the device increases and is released. Not only does the amount of heat increase and the efficiency (effective use of heat) of the hydrogen generator deteriorates, but also the cost increases due to the increase in size of the apparatus, and the value as a hydrogen generator decreases.
- the catalyst layer and the evaporation unit exchange heat uniformly with respect to the flow direction of the catalyst layer. It will be.
- a catalyst layer for example, a shift catalyst layer or a selective oxidation catalyst layer
- a shift reaction or a selective oxidation reaction takes place immediately upstream after entering the catalyst layer, so the temperature in the upstream portion of the catalyst layer rises due to heat of reaction.
- the temperature decreases due to heat exchange with the water evaporation part.
- the temperature is high in the upstream part of the catalyst layer and low in the downstream part.
- the catalyst characteristics are worse at high and low temperatures. Further, if the temperature becomes too high, the catalyst deteriorates at a high temperature, so it is necessary to use it at a temperature lower than the heat resistant temperature. If the temperature distribution is large in the catalyst layer, the catalyst characteristics may not be sufficiently secured.
- An object of the present invention is to provide a hydrogen generator capable of maintaining the temperature of at least one of the reforming catalyst layer, the shift catalyst layer, and the selective oxidation catalyst layer at an appropriate level and having stable performance. It is.
- a hydrogen generator is supplied by connecting a raw material supply unit that supplies a raw material gas, a water supply unit that supplies water, the raw material supply unit, and the water supply unit.
- a water evaporation unit that mixes water with water as a raw material gas, a fuel supply unit that supplies fuel gas, and an air supply unit that supplies combustion air; and a burner disposed inside the water evaporation unit
- a hydrogen generator provided with a carbon monoxide reduction unit that is disposed outside the carbon gas monoxide and is supplied with the reformed gas to reduce carbon monoxide in the reformed gas, wherein the water evaporation unit has the combustion exhaust gas flow Before the raw material gas and the outside of the road According to the heat exchange amount in
- the flow path member of the water evaporation section according to the amount of heat exchange in at least one of the combustion exhaust gas flow path and the water evaporation section or the water evaporation section and the carbon monoxide reduction section.
- FIG. 1 is a schematic configuration diagram showing a hydrogen generator according to Embodiment 1 of the present invention.
- Schematic configuration diagram showing a hydrogen generator according to Embodiment 2 of the present invention Characteristics of shift catalyst Characteristics of selective oxidation catalyst
- a hydrogen generator comprising: a raw material supply unit that supplies a raw material gas; a water supply unit that supplies water; and the raw material supply unit and the water supply unit that are connected to each other to supply water as water vapor A water evaporation part to be mixed, a fuel supply part for supplying fuel gas, and an air supply part for supplying combustion air, and a combustion exhaust gas from which the combustion exhaust gas from the burner is disposed inside the water evaporation part A flow path, a reforming catalyst layer that is supplied with a mixed gas from the water evaporation section and generates a reformed gas containing hydrogen by a steam reforming reaction of the reforming catalyst, and is disposed outside the water evaporation section
- a hydrogen generation apparatus comprising a carbon monoxide reduction unit that is supplied with a reformed gas and reduces carbon monoxide in the reformed gas, wherein the water evaporation unit is disposed outside the combustion exhaust gas passage.
- the flow path member has a flow path member and the flow path of the water evaporation section according to the amount of heat exchange in at least one of the combustion exhaust gas flow path and the water evaporation section or the water evaporation section and the carbon monoxide reduction section
- the pitch between the members is changed.
- the pitch between the flow path members of the water evaporation section depends on the heat exchange amount in at least one of the combustion exhaust gas flow path and the water evaporation section or the water evaporation section and the carbon monoxide reduction section.
- the second aspect of the present invention is the hydrogen generator according to the first aspect of the present invention, wherein the heat exchange amount in at least one of the combustion exhaust gas flow path and the water evaporation section or the water evaporation section and the carbon monoxide reduction section.
- the pitch between the flow path members of the water evaporation portion where it is desired to be increased is formed densely.
- the pitch between the flow path members of the water evaporation section where the heat exchange amount is desired to be increased is formed densely, so that the temperature of the reforming catalyst layer and the carbon monoxide reduction section is increased. It is possible to keep it appropriate and to stabilize the performance of the hydrogen generator.
- the downstream portion of the water evaporation portion is other than the downstream portion.
- the amount of heat exchange with the combustion exhaust gas flow path is larger than that of the point.
- the downstream portion of the water evaporation section has a configuration in which the amount of heat exchange with the combustion exhaust gas passage is larger than that of the portion other than the downstream section, whereby the reforming catalyst layer.
- the supply of liquid droplets can be prevented, and the performance of the hydrogen generator can be stabilized.
- the flow path member of the water evaporation section is sandwiched between a double cylinder and the double cylinder. It is comprised by the partition part of a spiral shape, and the pitch between the said partition parts is a thing small compared with locations other than the said downstream part in the downstream part of the said water evaporation part.
- the flue gas flow in the downstream part of the water evaporation part can be achieved with a simple structure by setting the pitch of the partition part in the downstream part of the water evaporation part to be smaller than that of the part other than the downstream part.
- the amount of heat exchange with the road can be increased.
- the hydrogen generator according to a fifth aspect of the invention is particularly the hydrogen generator according to the first or second aspect of the invention, wherein the carbon monoxide reducing section is supplied with the reformed gas and the reformed gas by a shift reaction of a shift catalyst.
- the heat exchange amount with the water evaporation unit is larger than that of the layer other than the upstream portion of the flow of the reformed gas.
- the amount of heat exchange with the water evaporation portion in the upstream portion of the shift catalyst layer is made larger than that in other portions, so that the temperature distribution of the shift catalyst is reduced and the entire shift catalyst has the most characteristics.
- the stable temperature operation of the hydrogen generator is realized by setting the temperature to be easily generated.
- the flow path member of the water evaporation section includes a double cylinder and a spiral-shaped partition portion sandwiched between the double cylinders.
- the partition portion is configured such that the pitch of the partition portion is smaller in the vicinity of the upstream portion of the shift catalyst layer than in the adjacent water evaporation portion other than the upstream portion of the shift catalyst layer.
- the pitch of the partition portion in the vicinity of the upstream portion of the shift catalyst layer is made smaller than that in the portion other than the upstream portion, so that the water evaporation portion in the upstream portion of the shift catalyst layer can be configured with a simple configuration.
- the amount of heat exchange can be increased.
- the carbon monoxide reducing section is supplied with the reformed gas and is supplied with the reformed catalyst by a shift reaction of the reformed gas.
- a conversion catalyst layer for reducing carbon oxide, and a selective oxidation catalyst layer for reducing the carbon monoxide in the conversion gas by the selective oxidation catalyst when the conversion gas flows from the conversion catalyst layer and the oxidant is supplied.
- the selective oxidation catalyst layer is adjacent to the outside of the water evaporation portion, and the upstream portion of the shift gas flow of the selective oxidation catalyst layer is closer to the water evaporation portion than the upstream portion of the selective oxidation catalyst layer other than the upstream portion.
- the heat exchange amount is increased.
- the amount of heat exchange with the water evaporation section in the upstream portion of the selective oxidation catalyst layer is made larger than that in the other portions, so that the temperature distribution of the entire selective oxidation catalyst is reduced and the entire selective oxidation catalyst is reduced. This is to achieve a stable operation of the hydrogen generator at a temperature state where the characteristics are most likely to appear.
- the hydrogen generator according to the seventh aspect wherein the flow path member of the water evaporation section has a double cylinder and a spiral shape sandwiched between the double cylinders.
- the partition portion is configured so that the pitch of the partition portion is smaller in the vicinity of the upstream portion of the selective oxidation catalyst layer than in the water evaporation portion adjacent to the portion other than the upstream portion of the selective oxidation catalyst layer.
- the pitch of the partition portion in the vicinity of the upstream portion of the selective oxidation catalyst layer is set to be smaller than that of the portion other than the upstream portion, whereby water evaporation in the upstream portion of the selective oxidation catalyst layer can be achieved with a simple configuration.
- the amount of heat exchange with the part can be increased.
- a fuel cell power generation device according to any one of the fourth, sixth and eighth aspects of the invention, wherein the spiral partition is formed of a metal round bar.
- the spiral partition portion can be configured with a simple configuration.
- a fuel cell power generator including the hydrogen generator according to any one of the first to ninth aspects. According to the tenth aspect, by mounting the hydrogen generator that realizes stable operation, the fuel cell power generator can be stably operated.
- FIG. 1 shows a hydrogen generator according to Embodiment 1 of the present invention.
- the hydrogen generator has a burner 4 that mixes the fuel gas supplied from the fuel gas supply unit 1 and the air supplied from the air fan 3 and sent through the air flow path 2 to form a flame. is doing.
- the combustion exhaust gas generated in the burner 4 flows through the combustion exhaust gas passage 16 inside the cylinder 100 and is exhausted from the exhaust port 13 to the outside of the apparatus.
- a water evaporation unit 7 is provided in which the source gas from the source gas supply unit 5 and the water from the water supply unit 6 are supplied, and the supplied water is mixed with the source gas as water vapor. ing.
- the water evaporating unit 7 forms a space between the round bars by sandwiching a metal round bar 8 that is a spiral partition between the cylinder 100 and the cylinder 101, and the source gas and water are formed along the round bar 8 in the space. It becomes the composition which distributes. Therefore, the space of the water evaporation section 7 is partitioned by a spiral round bar 8 and is formed as a spiral flow path that surrounds the outer periphery of the cylinder 100.
- the water evaporating section 7 has a metal round bar 8 that is a channel member through which the raw material gas and water flow outside the combustion exhaust gas channel 16.
- the whole apparatus is covered with the heat insulating material 17.
- the interval of the spiral pitch of the round bars 8 is configured to be smaller in the downstream part of the water evaporation part 7 than in the middle stream part or the upstream part.
- the mixed gas of the raw material and water vapor sent from the water evaporation unit 7 is supplied to the reforming catalyst layer 9 located below the water evaporation unit 7 outside the combustion exhaust gas flow path 16.
- the reformed gas delivered from the reforming catalyst layer 9 is supplied to the shift catalyst layer 10 disposed outside the water evaporation unit 7. Further, the shift gas sent from the shift catalyst layer 10 is mixed with the air from the selective oxidation air supply unit 14 in the selective oxidation catalyst layer 11 located above the shift catalyst layer 10 outside the water evaporation unit 7. Supplied.
- the product gas exiting the selective oxidation catalyst layer 11 is sent from the product gas outlet 12 as a product gas containing hydrogen at a high concentration of carbon monoxide of 10 ppm or less from the hydrogen generator.
- the shift catalyst layer 10 is supplied with a reformed gas and reduces carbon monoxide in the reformed gas by a shift reaction of the shift catalyst.
- the selective oxidation catalyst layer 11 is one in which the shift gas from the shift catalyst layer 10 flows in and carbon monoxide in the shift gas is reduced by the selective oxidation catalyst by supplying an oxidizing agent.
- the shift catalyst layer 10 and the selective oxidation catalyst layer 11 are referred to as a carbon monoxide reduction unit, but it is sufficient that at least the shift catalyst layer 10 is included.
- the fuel gas and air supplied to the burner 4, the raw material gas and water supplied to the water evaporation unit 7, and the selective oxidation air supplied to the shift gas from the shift catalyst layer 10 are the fuel gas supply unit 1 and the air fan 3.
- the source gas supply unit 5, the water supply unit 6 and the selective oxidation air supply unit 14 can be controlled by a signal from the control unit 15.
- the fuel gas supply unit 1, the air fan 3, the raw material gas supply unit 5, the water supply unit 6, and the selective oxidation air supply unit 14 are each supplied with a combustible gas such as fuel gas, raw material gas, water, or off gas. Or air) is adjustable.
- the configuration for adjusting the flow rate may be a supply pump (driving means) capable of changing the discharge flow rate of the supply, and the flow rate of the supply provided in the supply source and the downstream flow path.
- a fluid control mechanism combined with an adjustment valve may be used.
- the water evaporating unit 7 supplied with water and raw material evaporates water by heat exchange from the combustion exhaust gas in the combustion exhaust gas flow channel 16 flowing inside the water evaporation unit 7, and at the same time, the same flow of the water evaporation unit 7 Mixing with the raw material gas flowing in the passage is performed, and the mixed gas is supplied to the reforming catalyst layer 9.
- the reforming catalyst layer 9 is heated to a high temperature (generally 600 to 700 ° C.) by a high-temperature combustion exhaust gas flowing inside, and is supplied with a mixed gas of a raw material gas and steam so A reformed gas containing carbon oxide, carbon dioxide, etc. is generated.
- the shift catalyst layer 10 is maintained at an optimum temperature (150 to 300 ° C.) for the shift reaction by heat exchange with the water evaporation section 7 adjacent to the inside, and high concentration carbon monoxide (10 to 15%) in the reformed gas. ) Is changed to carbon dioxide to reduce the concentration of carbon monoxide (around 0.5%).
- the selective oxidation catalyst layer 11 is also maintained at a temperature optimum for the selective oxidation reaction (around 150 ° C.) by heat exchange with the water evaporation section 7 adjacent to the inside, and the air from the selective oxidation air supply section 14 is mixed with the shift gas.
- carbon monoxide in the metamorphic gas is in a very low concentration state of 10 ppm or less by a selective oxidation reaction.
- the control unit 15 changes the supply conditions in order to cope with the operating load. For example, when a command to change from a condition (TDR50) that generates 50% of the rated condition to a condition (TDR100) that generates the rated quantity of hydrogen (TDR100) is received, a signal from the control unit 15 causes a source gas supply unit 5, the water supply unit 6, and the selective oxidation air supply unit 14 are controlled to increase the raw material gas amount, the water supply amount, and the selective oxidation air amount.
- the water evaporation unit 7 increases the amount of water necessary for the TDR 100 from the condition where the water necessary for the TDR 50 is supplied.
- the amount of water required for TDR100 for example, 10 g / min
- the amount of water required for TDR50 for example, 5 g / min
- the water at room temperature (about 20 ° C.) supplied from the water supply unit 6 enters the water evaporation unit 7 and then the exhaust gas flowing through the combustion exhaust gas channel 16 and the heat of the selective oxidation catalyst layer 11, In response to the heat of the shift catalyst layer 10, the temperature is raised, and in the vicinity of the midstream portion of the shift catalyst layer 10, the evaporation is completely completed and becomes steam of 100 ° C. or higher.
- the evaporation of water is not completed near the middle portion of the shift catalyst layer 10 and is in a gas-liquid two-layer state at 100 ° C., and further flows downstream.
- the evaporation is completed at the outlet of the shift catalyst layer 10 and further downstream.
- the upstream portion of the reforming catalyst layer 9 rapidly increases from 400 ° C. to 100 ° C. The temperature drops. If a thermal shock due to such a temperature drop is applied to the catalyst, the catalyst may crack.
- the pitch of the spiral round bar 8 in the downstream portion of the water evaporation portion 7 is set to the water evaporation portion 7 in order to promote heat transfer in the downstream portion of the water evaporation portion 7 so that such a problem does not occur. It is made small compared with the places other than the downstream part.
- the helical round bar 8 formed in the downstream portion of the water evaporation portion 7 is made smaller in pitch than the portion other than the downstream portion of the water evaporation portion 7 to thereby form a spiral shape in the downstream portion of the water evaporation portion 7.
- the flow path becomes longer, the movement time of the water flowing through this spiral flow path becomes longer, and the amount of heat exchange between the downstream portion of the water evaporation section 7 and the combustion exhaust gas flow path 16 corresponding to this downstream section increases. is there. And since this heat exchange amount becomes large, water completely evaporates and the supply of droplets to the reforming catalyst layer 9 is prevented, and the performance of the hydrogen generator can be stabilized.
- the heat exchange amount as used in this Embodiment means the heat exchange amount per unit area.
- FIG. 2 shows a hydrogen generator according to Embodiment 2 of the present invention.
- the structure of the water evaporation part 7 differs from Embodiment 1 shown in FIG.
- the water evaporation section 7 is a metal round bar that is a spiral partition of the water evaporation section 7 adjacent to the upstream portion of the reformed gas flow in the shift catalyst layer 10.
- the pitch of 18 is smaller than the pitch of the spiral round bar 18 adjacent to the other part of the shift catalyst layer 10.
- the pitch of the metal round bar 18, which is a spiral partition portion, of the water evaporation part 7 adjacent to the upstream part of the flow of the shift gas in the selective oxidation catalyst layer 11 is selectively oxidized.
- the pitch is smaller than the pitch of the spiral round bar 18 adjacent to the other part of the catalyst layer 11.
- the reformed gas from the reformed catalyst layer 9 is supplied, so that 10% to 15% of CO in the reformed gas is reduced to 0.5% by the shift reaction.
- This shift reaction is an exothermic reaction and is a reaction that almost occurs in the upstream portion supplied to the shift catalyst layer 10.
- FIG. 3 shows a CO characteristic diagram with respect to the temperature of the shift catalyst. As shown in FIG. 3, it can be seen that the CO concentration increases even when the temperature is too high or too low.
- high-temperature reformed gas is supplied from the reforming catalyst layer 9 to the shift catalyst layer 10, and after the exothermic reaction in the upstream portion, the shift catalyst layer 10 conducts heat transfer to the water evaporation portion 7 and heat dissipation to the surrounding outside. Along with this, it flows to the downstream part, so the temperature decreases from the upstream part toward the downstream part.
- the CO concentration of the shift gas from the shift catalyst layer 10 becomes the concentration in the characteristics of FIG. 3 depending on the catalyst temperature at the shift catalyst layer 10 outlet. Therefore, if the temperature at the catalyst layer outlet becomes too low, CO in the metamorphic gas becomes 0.5% or more.
- the outlet of the shift catalyst layer 10 is configured so that the temperature of CO does not exceed 0.5%, but if the temperature at the outlet of the catalyst layer is set to a certain level so as not to decrease too much, the temperature of the upstream portion is accordingly increased. Also gets higher.
- a catalyst having a catalytic reaction Cu—Zn, Fe—Cr, etc.
- the pitch of the spiral round bar 18 is made smaller in the upstream portion of the shift catalyst layer 10 than in the upstream portion of the shift catalyst layer 10, and the water evaporation portion 7.
- the amount of heat exchange between the water evaporation portion 7 and the upstream portion of the shift catalyst layer 10 is increased by extending the time during which water and water vapor having low temperatures flow.
- the temperature of the shift catalyst layer 10 can be kept low without exceeding the heat-resistant temperature of the catalyst, and at the same time, the temperature of the downstream portion of the shift catalyst layer 10 can be maintained high, so that the hydrogen generator is stable. Characteristics can be maintained.
- the conversion gas from the conversion catalyst layer 10 and the air from the selective oxidation air supply unit 14 are supplied, so that 0.5% CO in the conversion gas is reduced to 10 ppm or less by the selective oxidation reaction. Reduced.
- This selective oxidation reaction is also an exothermic reaction, and occurs immediately after being supplied to the selective oxidation catalyst layer 11.
- FIG. 4 shows a CO characteristic diagram with respect to the temperature of the selective oxidation catalyst. It can be seen that the CO amount increases even when the temperature is too high or too low. Also in the selective oxidation catalyst layer 11, like the shift catalyst layer 10, in the selective oxidation catalyst layer 11, after the exothermic reaction in the upstream portion, heat transfer to the water evaporation portion 7 and heat dissipation to the outside of the surrounding area lead to the downstream portion from the upstream portion. The temperature decreases.
- the CO state at the outlet of the selective oxidation catalyst layer 11 is determined by the temperature of the upstream part.
- the upstream portion may be in a temperature state in which the CO characteristics in FIG. 4 are good.
- the temperature at the outlet of the selective oxidation catalyst layer 11 is lowered, and the generated gas after leaving the selective oxidation catalyst layer 11 is reduced. The temperature will also drop.
- the temperature of the product gas is too low and falls below the dew point, water vapor in the product gas may condense.
- the catalyst having a high temperature is deprived of heat due to re-evaporation of the dew condensation water, and the temperature is lowered.
- the amount of heat exchange between the water evaporation portion 7 and the upstream portion of the selective oxidation catalyst layer 11 is increased.
- the pitch of the spiral round bar 18 is made smaller in the upstream portion of the selective oxidation catalyst layer 11 than in the upstream portion of the selective oxidation catalyst layer 11, and the selective oxidation catalyst layer 11.
- the amount of heat exchange between the water evaporation section 7 and the selective oxidation catalyst layer 11 is increased by extending the time during which water or water vapor having a low temperature flows in the water evaporation section 7 as compared with other portions.
- the temperature of the reforming catalyst layer can be adjusted appropriately by changing the pitch of the water and by forming the pitch between the flow path members (round bars 8) of the water evaporation section 7 where the heat exchange amount is to be increased. Therefore, it is possible to stabilize the performance of the hydrogen generator.
- the heat exchange amount as used in this Embodiment means the heat exchange amount per unit area.
- the pitch of the spiral round bar 18 in the upstream portion of the shift catalyst layer 10 and the upstream portion of the selective oxidation catalyst layer 11 is made to be simultaneously reduced.
- the pitch may be reduced only in the 10 upstream portion, or the pitch may be reduced only in the upstream portion of the selective oxidation catalyst layer 11, or a configuration adapted to each hydrogen generator.
- the second embodiment and the first embodiment may be combined and implemented at the same time.
- the flow path in the water evaporation unit 7 is formed using the spiral round bars 8 and 18, but the partition function such as a spiral plate or pipe is used. Any channel may be used to form the flow path as long as water can flow without stagnation.
- the fuel cell power generator can be stably operated.
- the hydrogen generator of the present invention realizes a stable supply of hydrogen as a small, high-efficiency, low-cost device.
- an apparatus for supplying a hydrogen-containing product gas to a household fuel cell system Useful as.
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Abstract
Description
第9の発明によれば、簡素な構成で螺旋形状の仕切り部を構成することができる。
第10の発明によれば、安定運転を実現する水素発生装置を搭載することにより、燃料電池発電装置の安定運転が可能となる。
(実施の形態1)
図1は本発明の実施の形態1における水素発生装置を示すものである。水素発生装置は、燃料ガス供給部1より供給された燃料ガスと、空気ファン3から供給されて空気流路2を介して送られてきた空気とを混合して火炎を形成するバーナ4を有している。バーナ4で生じた燃焼排ガスは、円筒100の内側の燃焼排ガス流路16を流れ、排気口13より装置外に排気される。
バーナ4では、燃料ガスと空気との混合が行われ、その混合ガスに高電圧の放電を行う(構成を図示せず)ことで火炎を形成し、高温の燃焼排ガスをつくり出して燃焼排ガス流路16に供給している。
なお、本実施の形態でいう熱交換量は単位面積当たりの熱交換量の意味である。
図2は本発明の実施の形態2における水素発生装置を示すものである。図1に示す実施の形態1とは水蒸発部7の構成が異なっている。
なお、本実施の形態でいう熱交換量は単位面積当たりの熱交換量の意味である。
2 空気流路
3 空気ファン
4 バーナ
5 原料ガス供給部
6 水供給部
7 水蒸発部
8,18 丸棒
9 改質触媒層
10 変成触媒層
11 選択酸化触媒層
12 生成ガス出口
13 排気口
14 選択酸化空気供給部
15 制御部
16 燃焼排ガス流路
17 断熱材
100 円筒
101 円筒
Claims (10)
- 原料ガスを供給する原料供給部と、水を供給する水供給部と、前記原料供給部と前記水供給部とがつながり供給された水を水蒸気として原料ガスと混合する水蒸発部と、燃料ガスを供給する燃料供給部と燃焼用空気を供給する空気供給部が繋がるバーナと、前記水蒸発部の内側に配置され前記バーナからの燃焼排ガスが流れる燃焼排ガス流路と、前記水蒸発部からの混合ガスが供給されて改質触媒の水蒸気改質反応により水素を含む改質ガスを生成する改質触媒層と、前記水蒸発部の外側に配置され前記改質ガスが供給されて前記改質ガス中の一酸化炭素を低減する一酸化炭素低減部とを備えた水素発生装置であって、前記水蒸発部は前記燃焼排ガス流路の外側に前記原料ガスと前記水が流れる流路を構成する流路部材を有し、前記燃焼排ガス流路と前記水蒸発部あるいは、前記水蒸発部と前記一酸化炭素低減部の少なくともいずれか一方における熱交換量に応じて前記水蒸発部の前記流路部材間のピッチが変更される水素発生装置。
- 前記燃焼排ガス流路と前記水蒸発部あるいは、前記水蒸発部と前記一酸化炭素低減部の少なくともいずれか一方における熱交換量を大きくしたい所の前記水蒸発部の前記流路部材間のピッチが密に形成される請求項1記載の水素発生装置。
- 前記燃焼排ガス流路と前記水蒸発部における熱交換量において、前記水蒸発部の下流部が、前記下流部以外の箇所に比べて前記燃焼排ガス流路との熱交換量が大きくなる構成である請求項1または2に記載の水素発生装置。
- 前記水蒸発部の前記流路部材は、二重の円筒と前記二重の円筒にはさまれた螺旋形状の仕切り部により構成され、前記仕切り部間のピッチが前記水蒸発部の下流部では、前記下流部以外の箇所に比べて小さい請求項1~3のいずれか1項に記載の水素発生装置。
- 前記一酸化炭素低減部は、前記改質ガスが供給され変成触媒のシフト反応により前記改質ガス中の一酸化炭素を低減する変成触媒層を有し、前記変成触媒層は前記水蒸発部の外側に隣接し、前記変成触媒層の、前記改質ガスの流れの上流部が、前記変成触媒層の、前記改質ガスの流れの上流部以外に比べて、前記水蒸発部との熱交換量が大きくなる構成である請求項1または2に記載の水素発生装置。
- 前記水蒸発部の前記流路部材は、二重の円筒と前記二重の円筒にはさまれた螺旋形状の仕切り部により構成され、前記仕切り部のピッチが前記変成触媒層の上流部近傍では、前記変成触媒層の上流部以外に隣接する前記水蒸発部に比べて小さい請求項5記載の水素発生装置。
- 前記一酸化炭素低減部は、前記改質ガスが供給され変成触媒のシフト反応により前記改質ガス中の一酸化炭素を低減する変成触媒層と、前記変成触媒層からの変成ガスが流入し酸化剤の供給により選択酸化触媒によって変成ガス中の一酸化炭素を低減する選択酸化触媒層とを有し、前記選択酸化触媒層は前記水蒸発部の外側に隣接し、前記選択酸化触媒層の、前記変成ガス流れの上流部が、前記選択酸化触媒層の、前記上流部以外に比べ前記水蒸発部との熱交換量が大きくなる構成である請求項1または2に記載の水素発生装置。
- 前記水蒸発部の前記流路部材は、二重の円筒と前記二重の円筒にはさまれた螺旋形状の仕切り部により構成され、前記仕切り部のピッチが前記選択酸化触媒層の上流部近傍では、前記選択酸化触媒層の上流部以外に隣接する前記水蒸発部に比べて小さい請求項7記載の水素発生装置。
- 前記螺旋形状の前記仕切り部が金属の丸棒により構成されている請求項4、6および8のいずれか1項に記載の水素発生装置。
- 請求項1~9のいずれか1項に記載の水素発生装置を設けた燃料電池発電装置。
Priority Applications (6)
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CN2009801174012A CN102099285B (zh) | 2008-05-15 | 2009-05-13 | 氢发生器和燃料电池发电器 |
US12/992,338 US8815455B2 (en) | 2008-05-15 | 2009-05-13 | Hydrogen generator and fuel cell power generator |
KR1020107025636A KR101203454B1 (ko) | 2008-05-15 | 2009-05-13 | 수소 발생 장치 및 연료 전지 발전 장치 |
JP2010511884A JP5477748B2 (ja) | 2008-05-15 | 2009-05-13 | 水素発生装置及び燃料電池発電装置 |
EP09746366.5A EP2287112B1 (en) | 2008-05-15 | 2009-05-13 | Hydrogen generator and fuel cell power generator |
CA2724183A CA2724183A1 (en) | 2008-05-15 | 2009-05-13 | Hydrogen generator and fuel cell power generator |
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JP2008-128024 | 2008-05-15 | ||
JP2008128024 | 2008-05-15 |
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PCT/JP2009/002095 WO2009139159A1 (ja) | 2008-05-15 | 2009-05-13 | 水素発生装置及び燃料電池発電装置 |
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US (1) | US8815455B2 (ja) |
EP (2) | EP2287112B1 (ja) |
JP (1) | JP5477748B2 (ja) |
KR (1) | KR101203454B1 (ja) |
CN (1) | CN102099285B (ja) |
CA (1) | CA2724183A1 (ja) |
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WO2011108264A1 (ja) * | 2010-03-04 | 2011-09-09 | パナソニック株式会社 | 水素生成装置および燃料電池発電システム |
CN102822086A (zh) * | 2010-03-30 | 2012-12-12 | 吉坤日矿日石能源株式会社 | 氢制造装置以及燃料电池系统 |
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KR20120047545A (ko) * | 2010-11-04 | 2012-05-14 | 삼성에스디아이 주식회사 | 연료 개질 장치 |
CN104203397A (zh) * | 2011-12-06 | 2014-12-10 | Hy9公司 | 催化剂容纳反应器系统以及相关方法 |
CN111732078A (zh) * | 2020-06-28 | 2020-10-02 | 鄂尔多斯市国科能源有限公司 | 氢气提纯装置及方法 |
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- 2009-05-13 EP EP09746366.5A patent/EP2287112B1/en active Active
- 2009-05-13 CN CN2009801174012A patent/CN102099285B/zh active Active
- 2009-05-13 JP JP2010511884A patent/JP5477748B2/ja active Active
- 2009-05-13 EP EP13001895.5A patent/EP2615058B1/en active Active
- 2009-05-13 KR KR1020107025636A patent/KR101203454B1/ko not_active IP Right Cessation
- 2009-05-13 US US12/992,338 patent/US8815455B2/en not_active Expired - Fee Related
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WO2011108264A1 (ja) * | 2010-03-04 | 2011-09-09 | パナソニック株式会社 | 水素生成装置および燃料電池発電システム |
CN102781820A (zh) * | 2010-03-04 | 2012-11-14 | 松下电器产业株式会社 | 氢生成装置以及燃料电池发电系统 |
JP5123442B2 (ja) * | 2010-03-04 | 2013-01-23 | パナソニック株式会社 | 水素生成装置および燃料電池発電システム |
CN102822086A (zh) * | 2010-03-30 | 2012-12-12 | 吉坤日矿日石能源株式会社 | 氢制造装置以及燃料电池系统 |
CN102822086B (zh) * | 2010-03-30 | 2014-12-31 | 吉坤日矿日石能源株式会社 | 氢制造装置以及燃料电池系统 |
US9012098B2 (en) | 2010-03-30 | 2015-04-21 | Jx Nippon Oil & Energy Corporation | Hydrogen production apparatus and fuel cell system |
Also Published As
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JP5477748B2 (ja) | 2014-04-23 |
RU2458854C2 (ru) | 2012-08-20 |
EP2615058B1 (en) | 2015-11-04 |
KR20110008230A (ko) | 2011-01-26 |
CA2724183A1 (en) | 2009-11-19 |
EP2287112B1 (en) | 2015-04-29 |
US8815455B2 (en) | 2014-08-26 |
KR101203454B1 (ko) | 2012-11-21 |
EP2287112A4 (en) | 2012-06-06 |
CN102099285B (zh) | 2013-07-03 |
US20110065011A1 (en) | 2011-03-17 |
JPWO2009139159A1 (ja) | 2011-09-15 |
EP2615058A1 (en) | 2013-07-17 |
RU2010146222A (ru) | 2012-06-20 |
CN102099285A (zh) | 2011-06-15 |
EP2287112A1 (en) | 2011-02-23 |
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