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WO2013005699A1 - Générateur d'énergie et procédé de génération d'énergie - Google Patents

Générateur d'énergie et procédé de génération d'énergie Download PDF

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Publication number
WO2013005699A1
WO2013005699A1 PCT/JP2012/066821 JP2012066821W WO2013005699A1 WO 2013005699 A1 WO2013005699 A1 WO 2013005699A1 JP 2012066821 W JP2012066821 W JP 2012066821W WO 2013005699 A1 WO2013005699 A1 WO 2013005699A1
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WO
WIPO (PCT)
Prior art keywords
fuel cell
hydrogen
power generation
fluidized bed
heat
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2012/066821
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English (en)
Japanese (ja)
Inventor
堤　敦司
堤　香津雄
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Institute of Exergy Engineering Inc
University of Tokyo NUC
Original Assignee
Institute of Exergy Engineering Inc
University of Tokyo NUC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Institute of Exergy Engineering Inc, University of Tokyo NUC filed Critical Institute of Exergy Engineering Inc
Priority to JP2012549932A priority Critical patent/JP5286529B2/ja
Publication of WO2013005699A1 publication Critical patent/WO2013005699A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • 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
    • H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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 relates to a power generation apparatus combining a gasifier using a carbon-based fuel as a raw material and a fuel cell, and more particularly to a high efficiency power generation apparatus and a power generation method.
  • a fuel cell is a power generation device capable of continuously extracting electric power by supplying hydrogen and oxygen from the outside to a negative electrode and a positive electrode, respectively, and causing them to react.
  • the electric capacity is limited.
  • the fuel cell supplies the reducing agent and the oxidizing agent from the outside, there is no limitation on the electric capacity, and the fuel cell has a great feature in that power generation can be continuously performed.
  • a fuel cell is characterized by the absence of a combustion process in its power generation process, and hydrogen and oxygen react to form water, so it is said to be a power generation apparatus with a small load on the environment.
  • Patent Document 3 discloses a fuel cell combined cycle power generation system provided with a fluidized bed gas furnace and a fuel cell. That is, the fuel supplied to the fluidized bed gas furnace undergoes thermal decomposition in a high temperature range to produce a gas containing carbon monoxide and hydrogen which is an effective gas component for fuel cell power generation. In this case, the temperature rise from the temperature at the time of fuel injection to a high temperature range is performed by partially burning the fuel. The generated gas from the fluidized bed gas furnace is subjected to dust removal to remove ash and the like, and the reactor generates hydrogen gas, which is sent to the fuel cell to generate electricity.
  • gasification gas generated in a coal gasification furnace is reformed into hydrogen gas in a shift reactor, supplied to a fuel cell to be generated, and supplied to a gas turbine for generation Do.
  • the technology which generates steam using exhaust heat of a gas turbine, supplies this steam to a steam turbine, and generates electricity is indicated.
  • the fuel cell is excellent in environmental performance, it is an exothermic reaction, and it can not be said that the exergy rate is high.
  • the heat generated at the time of power generation is used, for example, for district heating and cooling, but the heat recovery is not sufficient.
  • the heat radiated from the fuel cell main body is energy which is difficult to recover as power in terms of energy. That is, under the present circumstances, the heat generated from the fuel cell at the time of power generation is not always used effectively.
  • ⁇ G can be extracted as electricity and T ⁇ S can be extracted as heat by setting the energy that the fuel originally has as ⁇ H.
  • ⁇ H reaction heat of formation, and it is a negative value in the case of an exothermic reaction such as a combustion reaction, and is also called a calorific value.
  • ⁇ G free energy, energy that can be taken out as work, and is called exergy as effective energy.
  • T ⁇ S is heat generated with the reaction, and is expressed by the product of entropy change and temperature. And as an ability to take out effective energy, ⁇ G / ⁇ H is called an exergy rate. The exergy rate can be referred to as theoretical efficiency.
  • FIG. 1 shows the relationship between the temperature T and the exergy rate ⁇ G / ⁇ H.
  • the exergy rate of the gas at 1500 ° C. is about 65%
  • the gas at 600 ° C. is about 43%. Even if waste heat power generation is accumulated, this efficiency can not be exceeded. That is, the exergy rate, which is the rate at which the energy of the gas is converted into electrical energy, decreases at the time of heat generation. As a result, the rate at which the energy of the gas is converted to electrical energy is reduced.
  • the exergy rate also depends on the pressure. The higher the pressure, the higher the exergy rate. From this, the exergy rate itself can be brought close to 1 if high temperature and high pressure can be maintained in the reaction process.
  • the object of the present invention is to solve the above-mentioned problems, and is to bring the power generation efficiency close to the exergy rate ⁇ G / ⁇ H.
  • a power generation apparatus comprises a fluidized bed gas furnace that generates a gas by heating a raw material containing carbon and / or hydrocarbons, and gasified in the fluidized bed gas furnace.
  • a power generation apparatus comprising: a shift reactor that generates hydrogen from product gas; and a fuel cell that generates power using hydrogen generated by the shift reactor, wherein the fuel cell is installed in the fluidized bed gas furnace There is.
  • the fluidized bed gas furnace includes the fluidized bed provided with the fluidized medium and the freeboard portion provided in the upper space of the fluidized bed.
  • the raw material supplied to the fluidized bed gas furnace contains carbon, hydrocarbon, or a mixture of carbon and hydrocarbon.
  • the raw material is a carbon source and also a reducing material.
  • the fluidized bed gas furnace is provided with a fluidized bed, and further, a dispersion plate is provided under the fluidized bed, and the fuel cell is disposed in the fluidized bed. Preferably, it is disposed downstream of the dispersion plate.
  • the fluid bed is filled with the fluid medium, and the fluid medium is held by the dispersion plate.
  • the fuel cell is disposed in the fluidized bed that is a component of the fluidized bed gas furnace.
  • solid particles made of sand or the like having a suitable size are disposed as a fluid medium.
  • the fluidized bed gas furnace it is preferable to use the heat generated by the power generation of the fuel cell, which is necessary to gasify the raw material. That is, according to this configuration, since the fuel cell is installed in the fluidized bed, the heat generated when the fuel cell reacts (power generation) is transferred without waste to the fluidized bed directly through the fluidized medium, effectively The heat required to gasify the feedstock in the fluidized bed gas furnace is provided. Usually, in a fluidized bed gasifier, gasification of the raw material is attempted by utilizing heat from partial combustion of the raw material.
  • the heat necessary for the gasification of the raw material does not use the heat from the combustion of the raw material, but uses the heat generated by the reaction (power generation) of the fuel cell.
  • the power generation apparatus according to the present invention is characterized in that there is no combustion process.
  • the intention of the present invention is to eliminate the combustion process as a means to bring the power generation efficiency closer to the exergy rate ⁇ G / ⁇ H.
  • the operation of extracting heat is eliminated, and the power generation efficiency becomes the exergy rate ⁇ G / ⁇ H which is the theoretical efficiency.
  • there is a means to decrease T ⁇ S and to increase ⁇ G That is, since ⁇ G is determined by the temperature and the pressure, T ⁇ S can be reduced and the value of ⁇ G / ⁇ H can be increased by raising the temperature and the pressure by forming a process.
  • gasification of a raw material in a gasification furnace requires heat for gasifying the raw material. This heat is obtained by the combustion of the raw material.
  • the feature of the present invention is that the gasification of the raw material does not require the combustion of the raw material.
  • combustion means a wide combustion process including partial combustion.
  • the raw material referred to in the present invention may be not only fossil fuels such as coal, oil, and natural gas, but also biomass and manure of livestock, etc., and is a reducing material other than hydrogen.
  • the raw material is preferably introduced into the fluidized bed gas furnace from a hopper or the like.
  • the steam generated during the power generation of the fuel cell is supplied to the fluidized bed gas furnace from a wind box disposed upstream of the dispersion plate.
  • a windbox at the bottom of the fluidized bed gas furnace, and the steam necessary for fluidizing the fluidized medium is blown into the fluidized bed from the windbox.
  • a fluidized medium such as high temperature sand is fluidized in the bed by hot air, and the raw materials etc. are pyrolyzed therein. Gasification is performed. If air is fed into the fluidized bed by a blower or the like, the oxygen contained in the air burns the raw material. As described above, if the combustion process is involved in power generation, an exergy loss occurs to cause a decrease in the exergy rate ⁇ G / ⁇ H. Also, if air is used for fluidization, nitrogen will also be heated.
  • the fluidization uses steam generated by the reaction (power generation) of the fuel cell. Since air is not externally taken in for fluidization, it is possible to prevent the decrease in the value of the exergy rate ⁇ G / ⁇ H. By using high pressure steam it is possible to keep the pressure in the fluidized bed gas furnace and its downstream high. The higher the pressure of the reaction, the higher the exergy rate.
  • steam generated by the power generation of the fuel cell is supplied to the shift reactor, and hydrogen is generated from the generated gas using the heat of the steam.
  • the shift reactor reforms the product gas to produce hydrogen to be supplied to the fuel cell.
  • reforming is to produce hydrogen from carbon monoxide in the product gas, and is usually supplied using steam as a heat source, and the shift reaction proceeds with the aid of a catalyst. Only hydrogen may be generated from the product gas.
  • the fuel cell generates high temperature water vapor during power generation.
  • the heat generated by the fuel cell can be effectively used without wasting it.
  • the gasification reaction is represented by the following formula (1)
  • the shift reaction is represented by the following formula (2).
  • the power generation apparatus preferably includes a generator driven by the steam turbine, which guides the steam generated by the power generation of the fuel cell to the steam turbine.
  • a condenser may be provided downstream of the steam turbine.
  • the provision of the condenser increases the heat drop and makes it possible to extract a large amount of power from the steam turbine.
  • an electrolysis tank having a sealed structure for electrolyzing exhaust gas of the steam turbine is connected to an exhaust outlet of the steam turbine, and hydrogen and oxygen generated by the electrolysis are used as the fuel It is preferable to supply the battery to generate electricity.
  • the electrolysis tank By providing the electrolysis tank, it is possible to produce and accumulate hydrogen using surplus power.
  • the exhaust heat of the exhaust can be effectively used, the heat loss can be suppressed. If hydrogen and oxygen are generated at normal pressure, they will work with the atmosphere, causing losses.
  • the electrolysis tank since the electrolysis tank has a closed structure, the internal pressure is maintained at a higher pressure than the atmosphere. For this reason, by producing hydrogen by electrolysis of water in the electrolysis tank, it is possible to prevent the loss of the expansion component to the atmospheric pressure that has occurred under normal pressure. That is, the pressure in the electrolysis tank increases, and the exergy rate increases accordingly.
  • the outside of the system means the outside of the power generation device according to the present invention, and means a tank for storage, a pipeline for gas transportation, or the like.
  • a control valve that controls the amount of hydrogen supplied to the fuel cell is provided between the shift reactor and the fuel cell. By adjusting the control valve, it is possible to adjust the amount of hydrogen supplied to the fuel cell in order to secure the amount of heat corresponding to the supply of the raw material.
  • the power generation apparatus includes a scale that measures the weight of the raw material, and a control device that controls the control valve, and the control device can gasify the raw material based on a signal from the scale.
  • a heat quantity calculation circuit that calculates the amount of heat required for the fuel cell
  • a hydrogen quantity calculation circuit that calculates the quantity of hydrogen required for power generation of the fuel cell based on the signal from the heat quantity calculation circuit
  • the output of the hydrogen quantity calculation circuit Preferably, a control valve control circuit is provided to control the control valve.
  • a power generation apparatus comprises a fluidized bed gas furnace which generates a gas by heating a raw material containing carbon and / or hydrocarbons, and a shift reaction which generates hydrogen from the gasified gas produced in the fluidized bed gas furnace.
  • Generator and a fuel cell generating electricity using hydrogen generated by the shift reactor, wherein the heat necessary for gasifying the raw material is not derived from the combustion of the raw material; Use the heat generated by power generation.
  • a power generation apparatus comprises a fluidized bed gas furnace which generates a gas by heating a raw material containing carbon and / or hydrocarbons, and a shift reaction which generates hydrogen from the gasified gas produced in the fluidized bed gas furnace.
  • Generator and a fuel cell generating electricity using hydrogen generated in the shift reactor, wherein the gas for fluidization in the fluidized bed gasifier is not supplied from the outside, The steam generated by the fuel cell's power generation is used.
  • the power generation method comprises the steps of generating power by a fuel cell, gasifying the raw material by the heat generated at the time of power generation of the fuel cell to generate generated gas, and generating power of the fuel cell
  • a shift reaction step of reforming the product gas to generate hydrogen by heat generated at the time, a step of supplying hydrogen generated in the shift reaction step to the fuel cell to generate electric power, and The step of supplying steam generated by the power generation to the steam turbine to generate power is included.
  • the fuel cell is installed in the fluidized bed.
  • the feedstock comprises carbon and / or hydrocarbons.
  • the method includes the steps of: supplying the fuel cell for power generation; and removing hydrogen not supplied to the fuel cell from the hydrogen generated in the shift reaction step.
  • the fuel cell is installed in a fluidized bed, and the raw material contains carbon and / or hydrocarbon. Then, a part of hydrogen generated in the fluidized bed gasification furnace and the shift reactor is supplied to the fuel cell to perform power generation, and the remaining hydrogen can be taken out as a product, so the method of cogeneration of hydrogen is called be able to.
  • FIG. 1 is a basic configuration diagram of a power generation device according to an embodiment of the present invention. It is a basic block diagram of the electric power generating apparatus which concerns on another embodiment of this invention. It is a control systematic diagram which controls the control valve of FIG. It is a flow sheet of the electric power generating apparatus which concerns on embodiment of this invention.
  • A) is a flow sheet which concerns on embodiment of FIG. 2
  • (b) is a flow sheet which concerns on embodiment of FIG.
  • Figure 2 is a diagram showing coal gasification fuel cell power generation energy conversion.
  • FIG. 2 is a diagram showing a basic configuration of a power generation device according to an embodiment of the present invention.
  • the fluidized bed gas furnace 8 mainly includes the wind box 3 serving as an intake of working gas, the fluidized bed 2 located downstream of the wind box 3, and the freeboard portion 7 located downstream of the fluidized bed 2 It has as.
  • the wind box 3 and the fluidized bed 2 are separated by a dispersing plate 4.
  • the raw material 1 is supplied to the fluidized bed 2 from a raw material feeder (not shown) and undergoes thermal decomposition in a temperature range of 400 ° C. to 1000 ° C. to produce a gas containing hydrogen, carbon monoxide and some hydrocarbons. .
  • hydrogen is an effective gas component for power generation by the fuel cell 6.
  • the temperature rise from the temperature at the time of charge to 400 ° C. to 1000 ° C. is performed using the heat generated by the reaction (power generation) of the fuel cell 6.
  • the non-combustible substance mixed in the raw material 1 is discharged from the fluidized bed 2.
  • the raw material 1 may be carbon, a hydrocarbon and a mixture thereof.
  • coal is used in this embodiment, fossil fuel other than coal or biomass may be used. It may be methanol and ethanol, or may be a polymer compound such as plastic.
  • the superheated vapor from the fuel cell 6 is fed into the wind box 3 to suspend and suspend the fluid medium 5 composed of solid particles on the dispersion plate 4.
  • the fluid medium 5 is silica sand, powder particles such as alumina or iron particles, or a mixture of these. Further, the fluid medium 5 may carry a catalyst that reduces water to produce hydrogen.
  • the fluid medium 5 has a function of performing heat transfer to the raw material 1 in the fluid bed 2.
  • a fuel cell 6 is installed in the fluid medium 5.
  • the gas generated in the fluidized bed 2 (hereinafter referred to as product gas GG) contains carbon dioxide, water vapor, carbon monoxide, hydrogen, and dust.
  • product gas GG contains carbon dioxide, water vapor, carbon monoxide, hydrogen, and dust.
  • the generated gas GG is sent to the dust collector 12 through the piping 11 via the free board unit 7.
  • the generated gas GG sent to the dust collector 12 has a temperature of approximately 400 ° C. to 650 ° C. at the inlet of the dust collector 12.
  • the thermal decomposition endothermic reaction proceeds, so the gas temperature is lower than that of the fluidized bed part.
  • the gas temperature at the freeboard portion 7 may be lower than 650 ° C.
  • air or oxygen may be supplied to the freeboard 7 to raise the gas temperature to avoid a tar problem.
  • a cyclone system can be used as the dust collector 12
  • a filter system may be adopted.
  • the filter system is preferable from the viewpoint of high dust collection.
  • a bag filter can be used as the dust collector 12, but a cyclone may be used and a ceramic filter may be disposed further downstream thereof.
  • Solids such as ash and alkali metal salts removed by the dust collector 12 are discharged from the discharge passage 13 out of the system.
  • the product gas GG from which the ash content and the like have been removed is sent to the shift reactor 17 via the pipe 14.
  • a corrosive gas removal device (not shown) may be provided between the precipitator 12 and the shift reactor 17 for removing corrosive gas such as hydrogen chloride and hydrogen sulfide contained in the product gas GG.
  • a catalyst for enhancing the reaction rate such as magnetite (Fe 3 O 4 ) or platinum is filled inside the shift reactor 17.
  • the high temperature steam generated by the reaction (power generation) in the fuel cell 6 is supplied to the shift reactor 17.
  • the shift reactor 17 uses the heat and moisture of the high temperature steam, the shift reactor 17 reacts carbon monoxide in the product gas GG with water to produce hydrogen.
  • This hydrogen is supplied to the anode (negative electrode) of the fuel cell 6.
  • This reaction formula is shown in the following formula (5).
  • a fuel gas containing hydrogen as a main component (hereinafter referred to as a fuel gas FG) generated in the shift reactor 17 is sent to a hydrogen tank 21 via a pipe 18. Further, carbon dioxide is discharged from the pipe 19 to the outside of the system.
  • the fuel gas FG mainly composed of hydrogen stored in the hydrogen tank 21 is sent to the anode of the fuel cell 6 at high pressure.
  • Oxygen is supplied from the oxygen tank 23 to the cathode of the fuel cell 6 through the pipe 25.
  • the utilization efficiency of the fuel gas FG inside the fuel cell is not 100%, so the exhaust from the anode of the fuel cell 6 contains water vapor which is the main component and some unreacted fuel gas. Hydrogen in unreacted fuel gas is recovered and supplied to the fuel cell again.
  • the heat generated from the fuel cell 6 is substantially equal to the heat absorption component of the gasification reaction, this heat can be used as a heat source for gasification in the fluidized bed gas furnace 8.
  • gasification can be performed without partially burning the raw material 1, so power generation with high energy efficiency can be achieved.
  • the hydrogen tank 21 is supplied with hydrogen from the shift reactor 17 and also supplied from the electrolysis tank 26.
  • the exhaust of the steam turbine 31 is connected to the electrolysis tank 26 through a pipe 35.
  • the exhaust gas supplied to the electrolysis tank 26 is warmer than the normal temperature, and the content of air is small, so that water suitable for electrolysis is supplied.
  • makeup water is supplied to the electrolysis tank 26 from a system (not shown).
  • the electrolysis tank 26 has a closed structure, the internal pressure is maintained at a higher pressure than the atmosphere. For this reason, by producing hydrogen by electrolysis of water in the electrolysis tank 26, it is possible to prevent the loss of the expansion component to the atmospheric pressure that has occurred under normal pressure.
  • the oxygen produced in the electrolysis tank 26 is sent to the oxygen tank 23 through the pipe 28.
  • the power 46 required for the electrolysis may be supplied from the generated power 42 of the fuel cell 6.
  • the fuel cell 6 generates electric power 42, water vapor and heat.
  • the electric power 42 can be transmitted from the fuel cell 6 through the electric power system.
  • the generated heat is transferred to the raw material 1 through the fluid medium 5 and becomes a heat source for gasification. Further, a part of the generated steam is introduced from the dispersion plate 4 of the fluidized bed 2 as a gas for fluidization of the fluidized bed 2 and a heat source for gasification.
  • Part of the high-temperature steam (superheated steam) generated in the fuel cell 6 is introduced from the windbox 3 of the fluidized bed 2 through the piping 34, supplied to the fluidized medium 5, and endothermic gasification in the fluidized bed 2 Contribute to the reaction.
  • Another part can be supplied to the steam turbine 31 to drive the steam turbine generator 32 and extract it as the generated power 44 of the steam turbine.
  • a condenser 33 is provided downstream of the steam turbine 31. By reducing the exhaust pressure, the heat drop is increased to increase the power generated by the steam turbine generator 32. Further, the steam leaving the steam turbine 31 is sent to the electrolysis tank 26 through the pipe 35 and becomes a supply source of heat and water for electrolysis.
  • the DC power 46 required for the electrolysis may separately supply surplus power or the like, but it is also possible to use a part of the generated power 42 of the fuel cell 6.
  • Hydrogen is also supplied to the hydrogen tank 21 from the electrolysis tank 26 via the pipe 27. At this time, since the temperature of hydrogen supplied via the pipe 27 is low, heat exchange with the high temperature hydrogen of the hydrogen tank 21 is desirable.
  • the heat exchanger 29 is for raising the temperature of low-temperature hydrogen by heat exchange.
  • the steam turbine 31 is driven by the surplus of the steam generated by the fuel cell 6 to generate power, this surplus steam can also be used for cooling and heating, and a so-called regional cooling and heating system is constructed. It is also possible. In this sense, this embodiment can be viewed as a power and heat cogeneration system.
  • FIG. 3 shows a basic configuration diagram according to another embodiment of the present invention.
  • the power generation apparatus mainly includes a fluidized bed gas furnace 8 in which a fuel cell 6 is installed in the fluidized bed 2, a dust collector 12 and a shift reactor 17.
  • the hydrogen generated in the shift reactor 17 is temporarily stored in the hydrogen tank 21, a part of which is supplied to the fuel cell 6, and the rest can be supplied to other facilities through the pipe 38.
  • a control valve 36 may be provided in the middle of the pipe 22 between the fuel cell 6 and the hydrogen tank 21 to adjust the amount of hydrogen supplied to the fuel cell 6.
  • a controller 52 may be provided to adjust the control valve 36.
  • the weight of the raw material 1 supplied to the fluidized bed gas furnace 8 is measured using a weigher 51.
  • the heat quantity calculation circuit 54 calculates the quantity of heat necessary for the gasification and shift reaction based on the signal from the weighing device 51 and the signal from the raw material property table 53.
  • the raw material characteristic table 53 includes statistical data of the calorific value of the raw material 1.
  • the hydrogen amount calculation circuit 56 calculates the amount of hydrogen required to generate the heat amount obtained by the heat amount calculation circuit 54.
  • a fuel cell characteristic table 55 holding the relationship between the calorific value of the fuel cell 6 and the amount of supplied hydrogen is used.
  • the controller 52 controls the control valve 36 via the control valve control circuit 57 to adjust it to the calculated amount of hydrogen.
  • the present embodiment is also a facility that produces hydrogen while performing power generation by the fuel cell 6, and therefore can be considered as a co-production system of power and hydrogen.
  • the heat of the fuel cell 6 is supplied to the steam turbine 31 and a part of the heat is recovered, but is discarded via the condenser 33, thereby avoiding the occurrence of energy loss Absent.
  • the hydrogen cogeneration power generation device shown in FIG. 3 since there is no energy loss due to waste heat, high power generation efficiency can be achieved.
  • FIG. 5 (a) shows a flow sheet of cogeneration of power heat, which co-produces power and heat.
  • FIG. 5 (b) shows a flow sheet of co-production of power hydrogen, which co-produces power and hydrogen.
  • the figures in the figure show the energy at each stage when the energy of coal is 100, and the figures in parentheses show the energy ratio and the exergy ratio.
  • co-production of power hydrogen (FIG. 5 (b)) has no such energy loss.
  • heat is always generated, and cogeneration to be used as heat is performed, or the generated heat is used to operate a heat engine having a lower temperature level.
  • the heat generated has been heat exchanged with combustion air to reuse primary energy, such as reusing heat.
  • Such types of heat generating power generation devices exchange heat and transfer heat to fuel and air, or use a cascade of heat to install a heat engine that operates in a lower temperature range to obtain more electrical energy. Although it has been devised to generate the problem, it can not be said that it is sufficient.
  • the amount of fuel supplied is changed to change the amount of power generation.
  • the exhaust gas loss is kept constant by performing air-fuel ratio control in which the amount of air is controlled at a constant rate to the fuel, but when the load decreases, the amount of heat release decreases little with respect to the calorific value, so the power generation efficiency decreases.
  • a boiler turbine generator a generator with 100% load and 40% power generation efficiency, with 33% load, the power generation efficiency drops to about 30%.
  • the power generation efficiency according to the present invention is the power generation efficiency by performing the gasification using the heat generation of the fuel cell, although the power generation efficiency of 70% calculated in the partial combustion gasification fuel cell combined power generation so far Increases to 89%.
  • Figure 1 shows the relationship between temperature and exergy rate. If thermal energy is generated by a chemical reaction, the process will reduce exergy. When the temperature is high, the exergy rate is high.
  • FIG. 6 is a schematic view of a fluidized bed gasifier, a shift reactor, and a fuel cell, which play a central role in the embodiment of the present invention.
  • coal is introduced into a high temperature fluidized bed to reduce steam to generate hydrogen and carbon monoxide. Since carbon monoxide reacts with water to form hydrogen and carbon dioxide, the following formula (6) is obtained as a whole.
  • C + 2 H 2 O + Q CO 2 + 2 H 2 (6)
  • Q represents the amount of heat necessary for the reaction, and is supplied by the amount of heat generated from the fuel cell installed in the fluidized bed.
  • Q indicates the calorific value associated with power generation, which is the same value as the amount of heat when carbon is gasified.
  • W is electrical energy. If these two equations are added, it becomes the following equation (8), and carbon reacts with oxygen and is converted to carbon dioxide and electrical energy.
  • C + O 2 CO 2 + W (8)
  • FIG. 7 shows an energy conversion diagram when gasification of coal, oil, biomass and the like is performed by the fuel cell.
  • the energy possessed by the raw materials is shown on the top, and the exergy is shown on the bottom.
  • Coal of energy 100 has 95 exergy.
  • Coal is supplied with water vapor and heat of exergy 17 energy 35 from the fuel cell to generate hydrogen of exergy rate 83% exergy 112 energy 135 at 900 ° C.
  • Hydrogen becomes 81 electric energy with 60% efficiency in the fuel cell (SOFC), and the remaining Exergy 17 energy 35 water vapor and heat are supplied to the fluid bed, and the Exergy 10 energy 19 heat and hydrogen steam turbine It generates 8 electricity at 40% efficiency by power generation.
  • a total of 89 electricity will be generated, making it a 94% generator based on an 89% exergy basis with a 89% generation efficiency.
  • the power generation device according to the present invention can be suitably used as a power generation device in a power plant of a commercial power grid. Moreover, it can be suitably used as a power generation device in a private power generation facility or a power generation device connected to a micro grid.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Sustainable Energy (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Electrochemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Fuel Cell (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention vise à améliorer le rendement de génération d'énergie, le taux d'exergie (ΔG/ΔH) devant être aussi proche de 1 que possible. Pour cette raison, le rapport à la chaleur (ΔG) doit être réduit et l'énergie d'entrée (ΔH) doit être autant que possible de l'énergie électrique. A cet effet, l'invention concerne un générateur d'énergie qui comporte un four à gaz à lit fluidisé pour une gazéification de matières premières comprenant du carbone et/ou des hydrocarbures, une pile à combustible installée à l'intérieur du four à gaz à lit fluidisé, et un convertisseur pour reformer le gaz généré par la gazéification dans le four à gaz à lit fluidisé pour produire de l'oxygène. Dans ce générateur d'énergie, la pile à combustible génère de l'énergie électrique à l'aide de l'hydrogène généré dans le convertisseur, et la chaleur nécessaire pour gazéifier les matières premières dans le réacteur à lit fluidisé est créée par la génération d'énergie électrique dans la pile à combustible.
PCT/JP2012/066821 2011-07-05 2012-06-30 Générateur d'énergie et procédé de génération d'énergie Ceased WO2013005699A1 (fr)

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JP2017137212A (ja) * 2016-02-03 2017-08-10 エクセルギー・パワー・システムズ株式会社 発電装置および発電方法
JP2022030460A (ja) * 2020-08-07 2022-02-18 株式会社堤水素研究所 水素製造装置
WO2023238015A1 (fr) * 2022-06-10 2023-12-14 金尚志 Système d'alimentation sans coupure en énergie d'hydrogène

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JP2002050387A (ja) * 2000-08-04 2002-02-15 Kawasaki Heavy Ind Ltd 固体有機物からのエネルギー発生装置
JP2005272530A (ja) * 2004-03-23 2005-10-06 Central Res Inst Of Electric Power Ind バイオマス発電システム
JP2005330370A (ja) * 2004-05-19 2005-12-02 Takuma Co Ltd 間接加熱式流動床ガス化装置
JP2006128006A (ja) * 2004-10-29 2006-05-18 Central Res Inst Of Electric Power Ind バイオマスの炭化ガス化高温型燃料電池発電システム
JP2008291081A (ja) * 2007-05-23 2008-12-04 Central Res Inst Of Electric Power Ind ガス化設備
JP2010013333A (ja) * 2008-07-07 2010-01-21 Tokyo Gas Co Ltd 大気中二酸化炭素の分離回収処理装置

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Publication number Priority date Publication date Assignee Title
WO2000027951A1 (fr) * 1998-11-05 2000-05-18 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
JP2002050387A (ja) * 2000-08-04 2002-02-15 Kawasaki Heavy Ind Ltd 固体有機物からのエネルギー発生装置
JP2005272530A (ja) * 2004-03-23 2005-10-06 Central Res Inst Of Electric Power Ind バイオマス発電システム
JP2005330370A (ja) * 2004-05-19 2005-12-02 Takuma Co Ltd 間接加熱式流動床ガス化装置
JP2006128006A (ja) * 2004-10-29 2006-05-18 Central Res Inst Of Electric Power Ind バイオマスの炭化ガス化高温型燃料電池発電システム
JP2008291081A (ja) * 2007-05-23 2008-12-04 Central Res Inst Of Electric Power Ind ガス化設備
JP2010013333A (ja) * 2008-07-07 2010-01-21 Tokyo Gas Co Ltd 大気中二酸化炭素の分離回収処理装置

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017137212A (ja) * 2016-02-03 2017-08-10 エクセルギー・パワー・システムズ株式会社 発電装置および発電方法
JP2022030460A (ja) * 2020-08-07 2022-02-18 株式会社堤水素研究所 水素製造装置
JP7118341B2 (ja) 2020-08-07 2022-08-16 株式会社堤水素研究所 水素製造装置
WO2023238015A1 (fr) * 2022-06-10 2023-12-14 金尚志 Système d'alimentation sans coupure en énergie d'hydrogène

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