WO2006073150A1 - 固体酸化物形燃料電池システムの起動方法 - Google Patents
固体酸化物形燃料電池システムの起動方法 Download PDFInfo
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- WO2006073150A1 WO2006073150A1 PCT/JP2006/300017 JP2006300017W WO2006073150A1 WO 2006073150 A1 WO2006073150 A1 WO 2006073150A1 JP 2006300017 W JP2006300017 W JP 2006300017W WO 2006073150 A1 WO2006073150 A1 WO 2006073150A1
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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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- H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
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- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
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- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
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- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M2008/1293—Fuel cells with solid oxide electrolytes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Definitions
- the present invention relates to a solid oxide fuel cell (SOFC) system. More specifically, the start-up of a SOFC system comprising a reformer for reforming a raw material for hydrogen production such as a hydrocarbon fuel to produce a reformed gas containing hydrogen, and a SOFC using the reformed gas as fuel. Regarding the method.
- SOFC solid oxide fuel cell
- the reforming types include partial acid reforming (POX), autothermal reforming (ATR) and water steam reforming (SR).
- POX partial acid reforming
- ATR autothermal reforming
- SR water steam reforming
- methane is taken as an example of a raw material for hydrogen production
- methane is decomposed by a reaction represented by CH + H 0 ⁇ CO + 3H to produce hydrogen.
- methane is separated by a reaction expressed as CH + 1/20 ⁇ CO + 2H.
- Patent Document 1 Japanese Patent Laid-Open No. 2003-272690
- the steam reforming reaction is a reaction with a relatively large endotherm, and the reaction is not substantially started unless the temperature is relatively high. Therefore, at start-up, the steam reformer, especially its The medium layer is heated to a high temperature of about 600 ° C, for example. In addition, SOFC is heated to a high temperature of, for example, about 800 ° C at the time of startup.
- An object of the present invention is that the reformer can be started up efficiently and in a short time without impairing the advantage of steam reforming that the hydrogen concentration in the reformed gas can be made relatively high.
- the object is to provide a startup method that can start the OFC system efficiently and in a short time.
- a reformer having a reforming catalyst for reforming a raw material for hydrogen production to produce a reformed gas containing hydrogen, and a solid oxide form using the reformed gas as a fuel
- a starting method of a solid oxide fuel cell system having a fuel cell
- a catalyst having a partial oxidation reforming function and a catalyst having a steam reforming function are used as the reforming catalyst.
- the steam reforming is performed by reducing the rate of the partial oxidation reforming reaction or stopping the partial oxidation reforming reaction.
- the temperature of the catalyst having the partial acid reforming function is raised to a temperature at which the partial oxidation reforming reaction can proceed with the combustion gas obtained by burning the raw material for hydrogen production, and the raw material for hydrogen production
- the temperature of the solid oxide fuel cell can be raised by supplying the combustion gas obtained by burning the gas to the power sword of the solid oxide fuel cell.
- step c the catalyst having the steam reforming function is heated by the combustion gas obtained by burning the reformed gas discharged from the anode of the solid oxide fuel cell, and the solid oxide fuel
- the temperature of the solid oxide fuel cell can be raised.
- a reformer having a reforming catalyst for reforming a raw material for hydrogen production to produce a reformed gas containing hydrogen, and a solid oxide form using the reformed gas as a fuel
- a starting method of a solid oxide fuel cell system having a fuel cell
- a catalyst having a partial oxidation reforming function and a catalyst having a steam reforming function are used as the reforming catalyst.
- the steam reforming is performed by reducing the ratio of the partial oxidation reforming reaction or stopping the partial oxidation reforming reaction.
- a method for starting a solid oxide fuel cell system is provided.
- the temperature of the catalyst having a partial acid / ole reforming function is raised to a temperature at which the partial oxidation reforming reaction can proceed with the combustion gas obtained by burning the raw material for hydrogen production, and the raw material for hydrogen production
- the temperature of the solid oxide fuel cell can be raised by supplying the combustion gas obtained by burning the gas to the power sword of the solid oxide fuel cell.
- the reformer can be started up efficiently and in a short time without impairing the advantage of steam reforming that the hydrogen concentration in the reformed gas can be made relatively high. Can start the S OFC system efficiently and in a short time.
- FIG. 1 is a flowchart showing an example of a SOFC system to which the activation method of the present invention can be applied.
- FIG. 2 is a flowchart showing another example of a SOFC system to which the activation method of the present invention can be applied.
- FIG. 3 is a flowchart showing another example of a SOFC system to which the activation method of the present invention can be applied.
- FIG. 4 is a flowchart showing another example of a SOFC system to which the activation method of the present invention can be applied.
- a material force capable of obtaining a reformed gas containing hydrogen by a partial acid reforming method or an autothermal reforming method and by a steam reforming method can be appropriately selected and used.
- compounds having carbon and hydrogen in the molecule such as hydrocarbons, alcohols and ethers can be used.
- Preferable examples that can be obtained at low cost for industrial use or consumer use include methanol, ethanol, dimethyl ether, city gas, LPG (liquid petroleum gas), gasoline, and kerosene. Of these, kerosene is preferable because it is easily available for industrial use and for consumer use and is easy to handle.
- a catalyst having a partial oxidation reforming function and a catalyst having a steam reforming function are used as a reforming catalyst.
- Steam reforming catalyst may be used as the reforming catalyst.
- only the autothermal reforming catalyst having both the partial oxidation reforming function and the steam reforming function may be used as the reforming catalyst.
- the reformer includes a reforming reaction section having a reforming catalyst and an external heating of the reforming reaction section. And a container through which the gas can be circulated.
- a reformer having a reforming reaction tube filled with a reforming catalyst and having a reforming catalyst layer formed therein as a reforming reaction section and having a container for accommodating the reaction tube inside can be used.
- a structure in which the reaction tube penetrates the container may be used.
- the reformer is connected to a line that supplies an oxygen-containing gas such as air, a raw material for hydrogen production, and water vapor to the reforming catalyst individually or appropriately mixed.
- a line for supplying the modified gas to the SOFC anode is also connected.
- a partial oxidation reforming catalyst is filled in the previous stage (upstream side) inside the reforming reaction tube, and a steam reforming catalyst is filled in the subsequent stage (downstream side) to form a reforming catalyst layer.
- the reforming catalyst layer can be formed by filling the autothermal reforming catalyst in the former stage inside the reaction tube and filling the steam reforming catalyst in the latter stage. Further, the reforming catalyst layer can be formed by filling only the autothermal reforming catalyst into the reaction tube.
- reformer basically one reformer may be used, but a plurality of reformers having different types of reforming catalysts are not necessarily required. It can also be used.
- a reformer having a reforming catalyst layer made of a partial oxidation reforming catalyst partial oxidation reformer
- a reformer having a reforming catalyst layer made of a steam reforming catalyst steam reformer
- Known catalysts can be used for the partial oxidation reforming catalyst, the steam reforming catalyst, and the autothermal reforming catalyst.
- the partial oxidation reforming catalyst include platinum-based catalysts
- examples of the steam reforming catalyst include ruthenium-based and nickel-based catalysts
- examples of the autothermal reforming catalyst include rhodium-based catalysts.
- the temperature at which the partial acidification reforming reaction can proceed is, for example, 200 ° C to 1000 ° C, and the temperature at which the steam reforming reaction can proceed is, for example, 400 ° C to 1000 ° C.
- the steam reforming reaction temperature can be, for example, 450 ° C to 900 ° C, preferably 500 ° C to 850 ° C, and more preferably 550 ° C to 800 ° C.
- the amount of steam introduced into the reaction system is defined as the ratio of the number of moles of water molecule to the number of moles of carbon atoms contained in the raw material for hydrogen production (steam / carbon ratio), and this value is preferably 0.5 to 10, More preferably, it is 1-7, and more preferably 2-5.
- the space velocity (LHSV) at this time is AZB when the flow rate in the liquid state of the raw material for hydrogen production is A (L / h) and the volume of the catalyst layer is B (L).
- This value is preferably 0. More preferably, it is set in the range of 0.1 to 10h, more preferably 0.2 to 5h- 1 .
- an oxygen-containing gas is added to the raw material in addition to steam.
- the oxygen-containing gas may be pure oxygen, but air is also preferred because of its availability.
- An oxygen-containing gas can be added to balance the endothermic reaction associated with the steam reforming reaction and to maintain a temperature of the reforming catalyst layer or SOFC or to generate a heat generation amount that can raise the temperature.
- the amount of the oxygen-containing gas added is preferably 0.05 to 1, more preferably 0.1 to 0 as the ratio of the number of moles of oxygen molecules to the number of moles of carbon atoms contained in the raw material for hydrogen production (oxygen Z carbon ratio). 75, more preferably 0.2 to 0.6.
- the reaction temperature of the autothermal reforming reaction is 450, for example. C ⁇ 900.
- the space velocity (LHSV) at this time is preferably selected in the range of 0.1 to 30, more preferably 0.5 to 20, and still more preferably 1 to 10.
- the amount of steam introduced into the reaction system is preferably 0.3 to 10, more preferably 0.5 to 5, more preferably 1 to 3 as the steam Z carbon ratio.
- SOFC a known SOFC force can be appropriately selected and used. It may be cylindrical or flat.
- the temperature at which SOFC can generate electricity is, for example, 500 ° C or higher and 1200 ° C or lower.
- Known components of the SOFC system having a reformer can be appropriately provided as necessary.
- Specific examples include a desulfurizer that reduces the concentration of sulfur in the raw material for hydrogen production, a vaporizer that vaporizes the raw material for hydrogen production, and a SOFC cathode.
- flow rate adjusting means such as valves for adjusting the flow rate of the fluid, or shutting off the fluid flow Z shutting off the flow path Z switching means ,
- Heat exchange 'heat exchanger for heat recovery
- vaporizer for vaporizing liquid
- condenser for condensing gas
- heating to externally heat various devices with steam, etc.Z heat retention means storage means for various fluids, instrumentation Air, electrical system, signal system for control, control device, electrical system for output and power.
- step a or i is performed by heating the catalyst having a partial oxidation reforming function to a temperature at which the partial oxidation reforming reaction can proceed by combustion heat or electricity.
- a partial oxidation reforming catalyst or an autothermal reforming catalyst can be used as the catalyst having a partial oxidation reforming function.
- Combustion heat can be obtained by combusting combustibles with a combustor as appropriate.
- combustibles can be combusted appropriately in a combustor, and the catalyst can be heated by heat exchange with the combustion gas.
- an electric heater can be used.
- An electric heater is provided in the reaction tube containing the catalyst, and the electric heater can be energized.
- the catalyst when the catalyst can be energized, such as a metal support catalyst, the catalyst itself can be energized and the catalyst itself can be heated. These heating methods may be used in combination as appropriate.
- the temperature of a water vaporizer, a hydrogen production raw material vaporizer, or the like can be increased by combustion heat or electricity, and steam generation or hydrogen production raw material can be vaporized.
- step a After step a, a partial oxidation reforming reaction is performed, the temperature of the catalyst having the steam reforming function is raised by the partial oxidation reforming reaction heat, and the reformed gas is supplied to the solid oxide fuel cell anode. By doing so, step b of raising the temperature of the solid oxide fuel cell can be performed.
- the steam reforming reaction may proceed together with the partial oxidation reforming reaction.
- Partial acid-reforming can be performed, and autothermal reforming can be performed.
- the temperature of the catalyst is raised by the heat of reaction, so in autothermal reforming, the heat generated by the partial acid reforming reaction exceeds the endotherm by the steam reforming reaction, generating a total heat! ⁇ .
- a steam reforming catalyst or an autothermal reforming catalyst can be used as the catalyst having a steam reforming function.
- the partial oxidation reformer When the partial oxidation reformer and the steam reformer are used separately, the partial oxidation reformer performs partial oxidation reforming, and the temperature is relatively high due to heat generated by the partial oxidation reforming reaction.
- the reformed gas can be supplied to the steam reformer to raise the temperature of the steam reforming catalyst.
- a raw material for hydrogen production and an oxygen-containing gas are supplied to the partial oxidation reforming catalyst (or autothermal reforming catalyst).
- the partial oxidation reforming catalyst or autothermal reforming catalyst.
- steam is also supplied to the reforming catalyst.
- steam can be supplied to the reforming catalyst as desired.
- the temperature of SOFC is raised by supplying the reformed gas obtained from the reformer, which has a relatively high temperature due to heat generated by the partial oxidation reforming reaction, to the anode of SOFC.
- Step C of heating the medium or autothermal reforming catalyst can be performed.
- This combustion heat can be used to preheat the oxygen-containing gas used for this combustion, to heat the SOFC, to preheat or vaporize the raw material for hydrogen production, and to generate steam.
- step c an oxygen-containing gas such as air is supplied to the SOFC power sword, and the reformed gas that has passed through the anode and the oxygen-containing gas that has passed through the power sword can be subjected to a combustion reaction.
- an oxygen-containing gas such as air
- a combustor capable of combusting the reformed gas as appropriate can be used.
- This combustor may be provided in a reformer that may be provided in a container that accommodates SOFC.
- a partial oxidation reforming reaction is performed, the temperature of the catalyst having the steam reforming function is raised by the partial oxidation reforming reaction heat, and the reformed gas is combusted to solidify the combustion gas.
- Step ii of heating the catalyst having a steam reforming function with the combustion gas obtained by burning the reformed gas while raising the temperature of the solid oxide fuel cell by supplying the power sword of the physical fuel cell It can also be done.
- the ratio of the partial oxidation reforming reaction is reduced or the partial oxidation reforming reaction is stopped to perform the steam reforming. Perform step d or iii. Even if the rate of partial oxidation reforming reaction is reduced or zero, the steam reforming catalyst (or autothermal reforming catalyst) is heated by the combustion gas obtained by burning the reformed gas in step c or step ii. Will continue.
- the ratio of the partial oxidation reforming reaction is reduced, preferably by stopping the partial acid reforming reaction and performing steam reforming to reduce the hydrogen concentration in the reformed gas. Can be relatively high.
- the supply amount of oxygen-containing gas such as air to the reforming catalyst is reduced or made zero, that is, O
- step b or ii Using a partial acid-oxide reformer and a steam reformer separately, in step b or ii, a raw material for hydrogen production or the like is supplied to the partial acid-oxide reformer and obtained from the partial oxidation reformer.
- the reformed gas to be supplied is supplied to the water vapor reformer, in step d or iii, the raw material for hydrogen production or the like can be supplied to the steam reformer without being supplied to the partial oxidation reformer. That is, in step d, the use of the partial oxidation reformer can be stopped by switching the gas flow path.
- reaction tube contains oxygen. If the supply of gas is stopped and the supply of steam is started or continued, the partial oxidation reforming reaction can be stopped and steam reforming can be performed.
- step e or iv can be performed in which power is generated by the fuel cell and the temperature of the fuel cell is raised by cell reaction heat. This step is preferably performed because the SOFC can be further heated.
- the power generated here may be output to the grid when the SOFC is linked to the grid. Alternatively, it may be used as power for auxiliary equipment such as a pump and a blower of a fuel cell system.
- Partial oxidation reforming (or autothermal reforming) can be started at a relatively low temperature, and the reforming catalyst is directly heated by the partial oxidation reforming reaction. It can be done promptly. In addition, after the temperature rise is completed, only steam reforming can be performed, or even if accompanied by a partial acid-sodium reforming reaction, the ratio can be reduced, so that the hydrogen concentration in the reformed gas is relatively high. can do. Further, since the temperature of the reformer is raised quickly, and the SOFC is heated using a high-temperature reformed gas that also provides the reformer power, the temperature of the SOFC can be raised quickly.
- the temperature of the partial oxidation reforming catalyst should be 200 ° C or higher from the viewpoint of promoting the progress of the partial oxidation reforming reaction.
- the preferred temperature is 250 ° C or higher, and the more preferred temperature is 300 ° C or higher.
- the temperature of the hydrogen production raw material supplied to the reformer or the gas containing the hydrogen production raw material and the temperature of the catalyst layer inlet of the reformer are used to suppress thermal decomposition of the hydrogen production raw material.
- the temperature is not more than 00 ° C. Further, the temperature is preferably higher than the temperature at which water and the raw material for hydrogen production are vaporized.
- Fig. 1 shows an example of a SOFC system to which the activation method of the present invention can be applied.
- the cylindrical SOFC 1 is accommodated in a container (SOFC accommodating container) 2.
- the figure shows only one SOFC, but many SOFCs are arranged.
- the SOFC container 2 is partitioned into a region (anode gas chamber) 2a and a region (here, combustion chamber) 2b by a partition plate 3 through which gas can flow so that gas can flow.
- the reformed gas is supplied to the region 2a, and the reformed gas is supplied to the region 2b through the partition plate 3.
- the partition plate through which gas can flow for example, a punching plate, a foam plate, or a woven plate made of a heat-resistant metal or ceramics can be used.
- the partition plate through which gas can flow is a member for preventing combustion in the region (anode gas chamber) 2a.
- the SOFC has a cylindrical shape with the inner side being the force sword side and the outer side being the anode side, one end (the lower end in the drawing) is closed, and the other end opens into the region 2b.
- the reformed gas obtained in the reformer is supplied to the region 2a and supplied to the anode of the SOFC (the outer surface of the cylinder).
- the air preheated by the air preheater 4 provided in the region 2b is supplied from the air supply pipe 5 to the SOFC power sword (the inner surface of the cylinder). in this way As a result, hydrogen in the reformed gas and oxygen in the air cause an electrochemical reaction to generate electricity.
- the anode gas (anode off-gas) after being used for power generation is supplied to the region 2b through the partition plate 3, and the power sword gas (power sword-off gas) after being used for power generation is the open end of the SOFC. Is supplied to the force region 2b, where they undergo a combustion reaction. That is, the region 2b functions as a combustion chamber. The air flowing through the air preheater 4 is preheated by this combustion heat.
- the air preheater 4 a known heat exchange structure capable of heating air with the combustion gas in the region 2b can be used.
- a reforming reaction tube 10a that houses a reforming catalyst is provided in the container 10b or through the container 10b.
- a partial oxidation reforming catalyst (or autothermal reforming catalyst) is filled in the former stage, and a steam reforming catalyst is filled in the latter stage to form a reforming catalyst layer.
- the reforming catalyst layer may be formed by filling only the autothermal reforming catalyst.
- a water vaporizer 20 that vaporizes water to generate steam
- a kerosene vaporizer 21 that vaporizes kerosene
- a start-up combustor 22 that is used in an initial stage of startup (step a) are provided.
- kerosene and air are supplied to the start-up combustor 22 to perform combustion.
- the combustion gas is supplied to the reformer vessel 10b and the reforming reaction tube 10a is heated. After the reforming reaction tube is heated, the combustion gas is led to the kerosene vaporizer 21 and the water vaporizer 20 in order, and the temperature is raised.
- combustor 22 known combustion means capable of burning kerosene, for example, a panner or the like can be used as appropriate.
- the same fuel as the raw material for hydrogen production is used as the fuel for the combustor, but this is not necessarily the case.
- the water vaporizer reaches a temperature at which steam can be generated
- the kerosene air heater reaches a temperature at which kerosene can be vaporized
- the reforming catalyst or autothermal reforming catalyst
- the temperature reaches a temperature at which the partial oxidation reforming reaction can proceed
- steam is generated by the water vaporizer
- kerosene is vaporized by the kerosene vaporizer
- steam, vaporized kerosene and air are mixed
- the reformed reaction tube 10a is mixed.
- Supply Note that steam is not required to perform the partial acid-reforming reforming reaction, but the point of view for preventing carbon deposition on the piping is the case where only partial oxidation reforming is performed. Even if it exists, it is preferable to mix steam.
- a vaporizer is provided for using kerosene, which is a liquid fuel, as a raw material for hydrogen production.
- kerosene which is a liquid fuel
- the raw material for hydrogen production is used. No vaporizer is required.
- a preheater may be provided in place of the vaporizer for the raw material for hydrogen production.
- a partial oxidation reforming reaction (autothermal reforming reaction accompanied by a steam reforming reaction) occurs. Due to the heat generated by the reforming reaction, high-temperature reformed gas is generated, and the temperature of the reformer is increased. In particular, the partial oxidation reforming catalyst itself is heated by the heat generation, and the subsequent steam reforming catalyst is also heated by the reformed gas.
- Combustion by the start-up combustor may be stopped when heat generation due to reforming occurs!
- the high-temperature reformed gas obtained from the reformer 10 is guided to the region 2a (anode gas chamber) of the container 2 that accommodates the SOFC, and raises the temperature of the SOFC.
- air is supplied to the SOFC power sword side through the air preheater 4 and the air supply pipe 5.
- the air discharged from the power sword causes a combustion reaction with the reformed gas supplied to the region 2b (combustion chamber) through the partition plate 3, and generates heat here. With this combustion heat, air is preheated by the air preheater 4 provided in the region 2b.
- the combustion gas discharged from the region 2b is led to the reformer vessel 10b, the reforming reaction tube 10a is heated from the outside thereof, and then led to the kerosene vaporizer 21 to vaporize kerosene, and then It is guided to the water vaporizer 20 to generate steam.
- a known heat exchange structure can be adopted as appropriate for the kerosene vaporizer and the water vaporizer.
- the temperature of the reformer and the SOFC can be increased by the heat generated by the reforming reaction and the combustion heat obtained by burning the reformed gas.
- FIG. 2 shows another example of a SOFC system to which the activation method of the present invention can be applied.
- SOFC area 2b simply functions as a header for collecting power sword off gas, and anode off gas and power sword off gas are supplied into the reformer vessel 10b (outside the reforming reaction tube). Combustion is performed, and an air preheater 4 is provided here.
- the region 2a and the region 2b are partitioned by a partition plate 103 incapable of gas flow.
- the anode off-gas can be burned in the reformer rather than being burned in the container containing the SOFC.
- the start-up operation can also be performed in the same manner as in Example 1 except that the reformed gas that also discharges the SOFC anode chamber power is combusted in the reformer.
- combustion means for burning the force sword off gas and the anode off gas for example, a burner surface combustor or the like can be used.
- FIG. 3 shows still another example of the SOFC system to which the activation method of the present invention can be applied.
- the reformer 10 the kerosene vaporizer 21 and the water vaporizer 20 are installed in the region 2b of the container for accommodating the 20-power SOFC.
- this reformer can be configured only by the reforming reaction section such as a catalyst reaction tube.
- a reformer having the same configuration as that of the reforming reaction tube of Example 1 is used.
- the combustion gas generated in the start-up combustor 22 is guided to the region 2b, and the temperature of the reformer, kerosene vaporizer, and water vaporizer can be increased by this combustion gas.
- the start-up operation can be performed in the same manner as in Example 1 except that the temperature of the reformer, kerosene vaporizer, and water vaporizer in the region 2b is increased by the combustion gas of the start-up combustor.
- FIG. 4 shows still another example of the SOFC system to which the activation method of the present invention can be applied.
- the cylindrical SOFC101 has an anode on the inside and a force sword on the outside.
- the inside of the container 2 is partitioned into a region 2a (functioning as an anode off-gas header) and a region 2b (forced sword gas chamber) by a partition plate 103 that cannot flow gas.
- Region 2b force A reformer 10, a starting water vaporizer 120a, and a starting kerosene vaporizer 12la are provided in the sword gas chamber.
- a start-up combustor 22 is provided outside the SOFC container 2, and the combustion gas is guided to the region 2b so that the reformer, the start-up water vaporizer, and the start-up kerosene vaporizer can be heated.
- a normal operation combustor 122 is provided, and the combustion gas of the combustor can heat the normal operation water vaporizer 120b and the normal operation kerosene vaporizer 121b.
- the reformer 10 has the same configuration as in the third embodiment.
- kerosene and air are supplied to the start-up combustor 22 to perform combustion.
- the combustion gas is supplied to the region 2b, and the temperature of the startup water vaporizer 120a, the startup kerosene vaporizer 121a, the reformer 10, and the SOFC101 is increased.
- the reformer, the start-up water vaporizer, and the start-up kerosene vaporizer reach predetermined temperatures, and the partial oxidation reforming catalyst (or autothermal reforming catalyst) reaches a temperature at which the partial oxidation reforming reaction can proceed.
- the partial oxidation reforming catalyst or autothermal reforming catalyst
- a partial oxidation reforming reaction autothermal reforming reaction accompanied by steam reforming reaction
- the reformed gas obtained in this reformer is supplied from the reformed gas supply pipe 105 to the anode of the SOFC 101 to raise the temperature of the SOFC.
- the reformed gas discharged from the anode to the region 2a is supplied to the start-up combustor 22 as fuel. At this time, the supply of kerosene to the start-up combustor 22 can be stopped.
- the reformed gas discharged from the region 2a is supplied to the normal operation combustor 122 instead of the start combustor 22.
- Air is supplied to region 2b.
- the oxygen concentration in the region 2b (force sword chamber) can be made equal to air.
- the air can be preheated as appropriate.
- the heat required for the steam reforming reaction can be supplied mainly by radiant heat of SOFC power.
- the reformer 10 is preferably arranged at a position where the radiant heat of SOFC can easily reach.
- Example 4 after the partial oxidation reforming catalyst (or autothermal reforming catalyst) reaches a temperature at which the partial oxidation reforming reaction can proceed, and steam generation and kerosene vaporization are possible, partial oxidation reforming is performed.
- the reformed gas is supplied from the reformed gas supply pipe 105 to the anode of the SOFC 101 to raise the temperature of the SOFC.
- Example 5 instead of supplying the reformed gas to the anode of the SOFC, the reformed gas is supplied as fuel to the start-up combustor 22 using the line shown by the broken line in FIG. Is burned and the combustion gas is supplied to area 2b (power sword gas chamber) to heat the SOFC.
- the combustion heat of the reformed gas can be used to heat the startup water vaporizer, the startup kerosene vaporizer, and the reformer.
- the supply of kerosene to the start-up combustor can be stopped.
- the reformed gas is not supplied to the anode of the SOFC. Therefore, when generating electricity with SOFC, the reformed gas is supplied to the anode. For example, when the SOFC reaches a temperature at which power generation is possible, use of the line indicated by the broken line is stopped, and the reformed gas is supplied from the reformer 10 to the anode via the reformed gas supply pipe 105. The reformed gas discharged from the anode to the region 2a can be supplied to the normal operation combustor 122. In addition, preheated air is appropriately supplied to the region 2b. This enables power generation with SOFC.
- the SOFC system can be activated in the same manner as in the fourth embodiment.
- the power sword When supplying combustion gas to the power sword as in Examples 4 and 5, the power sword is returned. From the viewpoint of preventing deterioration in the original atmosphere, it is preferable to perform combustion gas management so that the oxygen concentration of the combustion gas becomes a desired concentration.
- the oxygen concentration of the combustion gas is governed by the air ratio. The lower the air ratio (close to 1), the higher the combustion gas can be obtained, and the viewpoint power to shorten the startup time is also preferable. However, the higher the air ratio, the higher the oxygen concentration, which is advantageous for the chemical stability of the force sword member.
- the oxygen concentration of the combustion gas supplied to the power sword is preferably 1% (dry mole basis) or more, more preferably 3% (dry mole basis) or more, and more preferably 5% (dry mole basis) or more. preferable.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/813,444 US8623563B2 (en) | 2005-01-07 | 2006-01-05 | Method for starting-up solid oxide fuel cell system |
CA2594394A CA2594394C (en) | 2005-01-07 | 2006-01-05 | Method of starting-up solid oxide fuel cell system |
KR1020077017138A KR101102804B1 (ko) | 2005-01-07 | 2006-01-05 | 고체산화물형 연료전지 시스템의 기동 방법 |
DK06702116.2T DK1840997T3 (da) | 2005-01-07 | 2006-01-05 | Fremgangsmåde til at starte fastoxid-brændselscellesystem |
EP06702116.2A EP1840997B8 (en) | 2005-01-07 | 2006-01-05 | Method of starting solid oxide fuel cell system |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2005-002537 | 2005-01-07 | ||
JP2005002537A JP4767543B2 (ja) | 2005-01-07 | 2005-01-07 | 固体酸化物形燃料電池システムの起動方法 |
Publications (1)
Publication Number | Publication Date |
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WO2006073150A1 true WO2006073150A1 (ja) | 2006-07-13 |
Family
ID=36647626
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/JP2006/300017 WO2006073150A1 (ja) | 2005-01-07 | 2006-01-05 | 固体酸化物形燃料電池システムの起動方法 |
Country Status (8)
Country | Link |
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US (1) | US8623563B2 (ja) |
EP (1) | EP1840997B8 (ja) |
JP (1) | JP4767543B2 (ja) |
KR (1) | KR101102804B1 (ja) |
CN (1) | CN100521337C (ja) |
CA (1) | CA2594394C (ja) |
DK (1) | DK1840997T3 (ja) |
WO (1) | WO2006073150A1 (ja) |
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CA2594394C (en) | 2013-05-28 |
US8623563B2 (en) | 2014-01-07 |
EP1840997B8 (en) | 2013-06-26 |
EP1840997B1 (en) | 2013-05-22 |
JP2006190605A (ja) | 2006-07-20 |
CA2594394A1 (en) | 2006-07-13 |
US20090291335A1 (en) | 2009-11-26 |
DK1840997T3 (da) | 2013-08-05 |
EP1840997A1 (en) | 2007-10-03 |
JP4767543B2 (ja) | 2011-09-07 |
KR101102804B1 (ko) | 2012-01-05 |
CN101099256A (zh) | 2008-01-02 |
CN100521337C (zh) | 2009-07-29 |
KR20070091362A (ko) | 2007-09-10 |
EP1840997A4 (en) | 2011-11-30 |
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