WO2015012302A1 - Charcoal syngas manufacturing method and apparatus, and fuel cell power generation system using said manufacturing method and apparatus - Google Patents

Charcoal syngas manufacturing method and apparatus, and fuel cell power generation system using said manufacturing method and apparatus Download PDF

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Publication number
WO2015012302A1
WO2015012302A1 PCT/JP2014/069428 JP2014069428W WO2015012302A1 WO 2015012302 A1 WO2015012302 A1 WO 2015012302A1 JP 2014069428 W JP2014069428 W JP 2014069428W WO 2015012302 A1 WO2015012302 A1 WO 2015012302A1
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Prior art keywords
charcoal
water gas
gas
combustion chamber
superheated steam
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PCT/JP2014/069428
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French (fr)
Japanese (ja)
Inventor
正博 深澤
清美 和田
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富士古河Ｅ＆Ｃ株式会社
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Priority to JP2015528304A priority Critical patent/JPWO2015012302A1/en
Publication of WO2015012302A1 publication Critical patent/WO2015012302A1/en

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    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • 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
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/094—Char
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • 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
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/1646—Conversion of synthesis gas to energy integrated with a fuel cell
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/50—Manufacturing or production processes characterised by the final manufactured product

Definitions

  • the present invention relates to a production method and apparatus for producing a charcoal water gas from charcoal and water by a water gas reaction, and a fuel cell power generation system using the production method and apparatus.
  • Fuel cell power generation systems are being put to practical use as clean energy.
  • the type of fuel cell depends on the polymer solid electrolyte type (PEFC), phosphoric acid type (PAFC), molten carbonate type (MCFC), and oxide solid electrolyte type ( SOFC), etc., and the latter has a higher operating temperature.
  • PEFC polymer solid electrolyte type
  • PAFC phosphoric acid type
  • MCFC molten carbonate type
  • SOFC oxide solid electrolyte type
  • a PEFC having a relatively low operating temperature of about 80 ° C. is expected to be used in a distributed manner for home use (see Patent Document 1).
  • PAFC with an output of about 100 kW (operating temperature is about 200 ° C.) is expected to be used as a medium- and small-scale distributed power source.
  • MCFC operating temperature is about 650 to 700 ° C.
  • SOFC operating temperature is about 900 to 1000 ° C.
  • city gas (13A gas) has been generally used as a fuel gas for small and medium-sized distributed fuel cells such as PEFC and PAFC.
  • fuel cells using digestion gas obtained by methane fermentation from naphtha, LP gas, and sewage sludge are also known (see Patent Document 2).
  • the components of the city gas are generally methane (CH 4 ) 89.6 [%] ethane (C 2 H 6 ), although there are some differences depending on the gas companies.
  • CH 4 methane
  • ethane C 2 H 6
  • the methane concentration in methane gas derived from sewage sludge is said to be about 60%.
  • LPG liquefied petroleum gas
  • Patent Document 3 In addition to the fuel gas, use of woody biomass fuel is also being studied (see Patent Document 3).
  • paragraph [0003] of Patent Document 3 the following is described as a power generation method using biomass fuel. That is, “(1) A method in which biomass fuel is directly burned in a boiler, for example, power generation by a steam turbine; (2) Fermentation of biomass fuel using microorganisms to extract methane gas, for example, a gas engine, a dual fuel diesel engine (3) Biomass resources are gasified in a gas generation furnace to generate a combustible gas, and this gas is supplied to, for example, a gas engine or a dual fuel diesel engine to generate electricity. There is a system etc. ".
  • biomass fuel is introduced into a gasifier, and oxidation, reduction reaction, and the like are performed using CO, H 2 , CH 4 , C 2 H 6, and the like. It is described that gas is generated and power is generated using the generated gas.
  • the manufacturing method and apparatus for producing a charcoal water gas from the charcoal and water by a water gas reaction have been completed to some extent due to the history of automobiles using charcoal (charcoal bus).
  • the inventors of the present application have also developed a system for generating electricity by driving a gasoline engine for automobiles in the form of a gas engine using charcoal water gas, and have completed a demonstration experiment.
  • the charcoal water gas is produced by a water gas reaction from charcoal (3C 10 H 5 O + C 30 H 20 O 3 ) obtained by making wood (2C 42 H 60 O 28 ) and water (H 2 O). Its composition is a mixed gas of hydrogen gas (H 2 ) of about 60 [%], carbon monoxide (CO) of about 20 [%], remaining carbon dioxide (CO 2 ), and methane gas (CH 4 ).
  • H 2 hydrogen gas
  • CO carbon monoxide
  • CH 4 methane gas
  • the water gas reaction of charcoal is an endothermic reaction, and it is essential to supply the necessary heat energy.
  • city gas is used at the time of start-up in the reformer, and heat energy is supplied using off-gas in the fuel cell operation after start-up.
  • this method there is a large difference in the calorific values of both gases, and it is necessary to burn with the same burner because of the structure, and advanced control technology is required to ensure its stability.
  • charcoal water gas reaction charcoal water gas is made from charcoal (solid) and water, so the heat energy required for endothermic reaction can be easily secured by burning a part of charcoal. . Further, the control regarding the combustion is facilitated by making it visible.
  • FIGS. 7 and 8 show a schematic configuration of a conventional charcoal water gas generator and a reaction form of charcoal water gas generation.
  • Conventional devices generally have an oxide layer (hereinafter also referred to as a combustion chamber). ),
  • a vertical charcoal water gas generator composed of a reducing layer and a dry layer is configured to generate charcoal water gas by supplying water from the outside below the oxide layer.
  • FIG. 7, FIG. 8 the structure of an apparatus and the reaction form of charcoal water gas generation
  • a vertical charcoal water gas generator 51 shown in FIG. 7 includes a charcoal filling part 52, a grate 53 provided below the charcoal filling part 52, and a take-out device 58 for taking out the charcoal water gas G from above the charcoal filling part 52.
  • the charcoal filling section 52 includes an oxidation layer (combustion chamber) 7a, a reduction layer 9a, and a dry layer 10a.
  • a burned charcoal ash layer 11a is Below the grate 53.
  • a burning port 54, a combustion chamber inspection port 55, and a refractory material 56 surrounding the combustion chamber side wall are provided below the charcoal water gas generator 51, and Is provided with a gas inspection torch 57 for confirming the generation of charcoal water gas.
  • the take-out device 58 is provided with a filter 60 for removing dust in the gas.
  • the filter 60 includes, for example, a coke layer and a layer such as a gold scrubber.
  • the combustion air A and the water W are supplied below an apparatus. Then, the water is heated by the combustion heat of the charcoal, and by the water gas reaction between the water and the charcoal, the charcoal filling gas 52 mainly generates the H 2 ⁇ CO gas-based charcoal water gas in the reduction layer 9a, The charcoal water gas G is taken out from the take-out device 58 via the dry layer 10a.
  • the combustion of the oxide layer 7a is performed so that the temperature zone of each part is maintained at about 900 to 1300 ° C for the oxide layer 7a, 800 to 900 ° C for the reduction layer 9a, and 600 to 800 ° C for the dry layer 10a. Control the degree. Combustion is started by igniting a suitable combustion auxiliary material in the outlet 54 below the oxide layer. After the ignition, it is confirmed by ignition in the gas inspection torch portion 57 that the internal temperature condition is established and the charcoal water gas is generated.
  • FIG. 8 is created with reference to Kozo Shionoya's “Charcoal Vehicle” (published by Power Corporation in 1996).
  • the aforementioned oxide layer 7a, reduction layer 9a, dry layer 10a, and ash layer 11a are schematically shown on the left side, and the chemical reaction in each layer is shown on the right side.
  • C + O 2 ⁇ CO 2 complete combustion of carbon
  • 2C + O 2 ⁇ 2CO incomplete combustion of carbon
  • C + CO 2 ⁇ 2CO reduction reaction
  • C + H 2 O ⁇ CO + H 2 and C + 2H 2 O ⁇ CO 2 + 2H 2 water gas reaction
  • CO + H 2 O ⁇ CO 2 + H 2 shift reaction
  • Reactions of CO + 3H 2 ⁇ CH 4 + H 2 O and C + 2H 2 ⁇ CH 4 are performed.
  • the reduction reaction and the water gas reaction are endothermic reactions. Therefore, in order to perform the reaction properly, heat supply is required, and this heat supply is caused by the combustion heat in the oxide layer 7a. Done.
  • the charcoal water gas is a mixed gas mainly containing H 2 ⁇ CO gas and containing CO 2 ⁇ CH 4 .
  • the composition is a mixed gas of hydrogen gas (H 2 ) approximately 60 [%], carbon monoxide (CO) approximately 20 [%], the remaining carbon dioxide (CO 2 ), and methane gas (CH 4 ).
  • Patent Document 4 describes an improved technique related to a production method and apparatus for producing the above charcoal water gas. It also describes the use of charcoal water gas for power generation devices.
  • Patent Document 4 states that “carbonization without consuming fossil fuel at all, and that the controllability of the carbonization temperature and the controllability of high-temperature carbonization are improved.
  • the charcoal is heated to a temperature of 800 ° C to 1200 ° C, it is brought into contact with air and water vapor to cause a gasification reaction to generate a large amount of combustible gas.
  • a charcoal gas is produced, and the object to be treated is heated by a combustion gas obtained by burning the charcoal gas in the combustion gas generation and supply means 3 to perform carbonization treatment.
  • this charcoal gas is used to perform gas power generation by the power generation means 12, and the carbonization processing system equipment is operated with the obtained electric power.”
  • Patent Document 4 describes in the embodiment of FIG. 1 or FIG. 2 that “the charcoal gas generated in the carbonization furnace 2 or the gasification furnace 10 generates water vapor by heating water through a heat exchanger. Is introduced into the upper part of the carbonization furnace 2 or the lower part of the gasification furnace 10 to perform a charcoal water gas reaction ".
  • JP 2002-124288 A Japanese Patent Laid-Open No. 11-126629 JP 2006-83293 A JP 2003-253278 A
  • the present invention has been made in view of the above points, and its purpose is to improve the stability of the water gas reaction and the gasification efficiency, and to improve the operation controllability when combined with a fuel cell.
  • a vertical cylindrical charcoal water gas generator having an oxidation layer (combustion chamber), a reduction layer, and a dry layer, and charcoal, water, and air are supplied to the charcoal water.
  • a method for producing a charcoal water gas by a water gas reaction from charcoal and water using a charcoal water gas production device comprising each supply means for supplying to the gas generator,
  • the reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, and a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to increase the temperature.
  • the high-temperature superheated steam is generated, and the water gas reaction is performed by introducing the superheated steam into the reduction layer.
  • the temperature of the superheated steam is preferably different depending on the charcoal used.
  • the reason for this is that the water gas reactivity and water gas shift reactivity fluctuate depending on charcoal properties such as refinement and pore area in the temperature zone of the reducing layer (800-900 ° C), so the reaction is controlled appropriately. This is because it is preferable to set the temperature of the superheated steam to a different temperature depending on the nature of the charcoal used.
  • a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer, and a dry layer, charcoal, water
  • the charcoal water gas production apparatus comprising each supply means for supplying air to the charcoal water gas generator,
  • the reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to High pressure superheated steam is generated, and the superheated steam and CO 2 gas generated by the combustion of charcoal in the combustion chamber are introduced into the reduction layer, and the combustion chamber is
  • the heat transfer wall and the lower cylindrical part are formed, the reduction layer is formed by the heat transfer wall and the upper cylindrical part, and the dry layer is formed by the upper cylindrical part, and the upper cylindrical part is formed on the upper cylindrical part.
  • the lower cylindrical part is provided with a charcoal inlet and combustion air inlet
  • the upper lid part of the upper cylindrical part Shall be provided with a charcoal inlet
  • the heat exchanger provided in the combustion chamber is formed by spirally winding a tube inside the cylinder of the lower cylindrical portion, and water is passed through the tube. From the viewpoint of simplifying the configuration of the heat exchanger, it is preferable.
  • a lattice is provided below the reducing layer and the combustion chamber arranged in the concentric cylindrical shape, and CO 2 gas generated by combustion of the charcoal is introduced into the reducing layer through a gap between the lattice, and this It is preferable to discharge ash generated with combustion below the grid.
  • the superheated steam is introduced into the reduction layer through the lattice from below the reduction layer, or through the upper lid and the dry layer from above the reduction layer. It is preferable to do so.
  • a charcoal water gas production comprising a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer and a dry layer, and each supply means for supplying charcoal, water and air to the charcoal water gas generator.
  • Apparatus a superheated steam generator that superheats water by combustion heat of charcoal generated in the combustion chamber to generate high-temperature and high-pressure superheated steam, and a charcoal water gas generated in the charcoal water gas production apparatus
  • a charcoal water gas fuel cell power generation system comprising a fuel cell device that generates electricity by supplying a fuel gas as a fuel gas, The superheated steam generated in the superheated steam generator is introduced into a reduction layer of the charcoal water gas generator so as to cause a water gas reaction.
  • the charcoal water gas generator and the superheated steam generator are combined, and superheated steam generated in the superheated steam generator is introduced into the reduction layer of the charcoal water gas generator.
  • the apparatus for causing the water gas reaction to be performed is an integrated charcoal water gas production apparatus, and the integrated apparatus is an apparatus according to any one of the aforementioned charcoal water gas production apparatuses. It is characterized by.
  • a CO reformer for reforming CO contained in the charcoal water gas is provided between the charcoal water gas generator and the fuel cell device, and the CO reformer is provided with the superheated steam generator. It is preferable to supply the generated superheated steam so that a shift reaction for shifting CO to CO 2 is performed.
  • the fuel cell is a PEFC, PAFC, or the like, it is not preferable to include CO in the fuel gas from the viewpoint of deterioration of the electrode catalyst. Therefore, the shift reaction is preferably performed.
  • a gas cooler or a gas heating device for cooling or heating the charcoal water gas is provided between the charcoal water gas generator and the fuel cell device according to the operating temperature of the fuel cell device.
  • a gas cooler is required, and when the fuel cell is an MCFC or SOFC, particularly a SOFC, a gas heating device is required.
  • a fuel cell off-gas utilization device for utilizing the energy of the residual gas (off gas) of the charcoal water gas that has not been consumed in the fuel cell device.
  • heat supply for the charcoal water gas reaction can be performed by heat transfer through a heat transfer wall of combustion heat generated in the combustion chamber, combustion exhaust gas, Because it uses the heat of superheated steam, etc., it is possible to achieve an appropriate and stable heat supply, and the control of the heat supply will be unified, so the charcoal water gas reaction temperature zone can be maintained more stably than in the prior art. Can control. As a result, the thermal efficiency of the charcoal water gas generation is improved, and as described later in detail, the operation controllability when combined with the fuel cell can be improved.
  • the above production method can be carried out with a simple configuration, and the controllability is also improved.
  • the charcoal water gas is used as the fuel gas of the fuel cell
  • the conventional fuel cell power generation system that is, city gas, sewage sludge-derived methane gas, woody biomass fuel, etc.
  • the above-described charcoal water gas production apparatus it is possible to improve efficiency and improve operation controllability.
  • a fuel cell power generation system using charcoal water gas has not been implemented conventionally. Therefore, although partially overlapping with the above description, the technical and social superiority of the charcoal water gas fuel cell power generation system is listed as follows. (1) The use of charcoal water gas makes the greenhouse gas (especially CO 2 ) free, and the only waste from the fuel cell is water. (2) Since noise reduction can be easily realized, it can be installed close to the power demand destination and can be diversified as a distributed energy facility in the region, which has a great merit for social use. (3) The entire facility can be made compact. (4) Good controllability of the entire equipment and easy handling.
  • Forest land can be optimized by promoting the use of thinned wood, and there is a social merit that can contribute to forest restoration.
  • the schematic cross section of the charcoal water gas manufacturing apparatus by embodiment of this invention The sectional side view of the charcoal water gas manufacturing apparatus by the Example of this invention.
  • 1 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to an embodiment of the present invention.
  • 1 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to a different embodiment of the present invention.
  • FIG. 1 is a schematic cross-sectional view of a charcoal water gas production apparatus according to an embodiment of the present invention
  • FIG. 2 is a side cross-sectional view of a charcoal water gas production apparatus according to an embodiment of the present invention
  • FIG. It is a sectional side view of the charcoal water gas manufacturing apparatus by a different Example.
  • the charcoal water gas production apparatus shown in FIG. 1 includes a charcoal water gas generator 1, supply means (not shown) for supplying charcoal, water, and air to the gas generator, a temperature measurement device and an operation control device, and an overheat It consists of water vapor introducing means (shown in FIGS. 2 and 3).
  • the charcoal water gas generator 1 includes a charcoal inlet top lid 2, a combustion air suction port 3 at startup, a charcoal inlet / combustion air hole 4, an ash outlet 5, a grid 6, an oxide layer (combustion chamber) 7, a reduction Layer 9, dry layer 10, ash layer 11, water pipe 12 as heat exchanger, lower cylindrical part 13, charcoal water gas outlet 14, upper cylindrical part 15, heat transfer wall 16, lower cylindrical part 13 and upper part A flange coupling part 17 with the cylindrical part 15 is provided.
  • FIGS. 2 to 3 is an embodiment of the apparatus for producing charcoal water gas according to FIG. 1, and a part of the description is omitted or added.
  • the embodiment of FIG. 2 is an embodiment provided with superheated steam introduction means 18 configured to introduce superheated steam generated in a water pipe 12 as a heat exchanger through the lattice 6 from below the reducing layer 9.
  • FIG. 3 shows an embodiment provided with superheated steam introducing means 18a which is introduced through the upper lid portion 2 and the dry layer 10 from above the reducing layer 9. From the viewpoint of structure, introduction from above is simple and advantageous, but from the viewpoint of heat loss, introduction from below is advantageous.
  • the introduced superheated steam S flows upward from the introduction portion of the superheated steam S and diffuses by the suction action of the gas flowing out from the charcoal water gas outlet 14.
  • the fundamental difference between the charcoal water gas generator 1 shown in FIG. 1 and the conventional charcoal water gas generator 51 shown in FIG. 7 is the arrangement relationship of the oxidation layer and the reduction layer.
  • the reducing layer is arranged vertically in the vertical direction, in the case of the charcoal water gas generator 1 shown in FIG. 1 according to the present invention, it is arranged concentrically below the apparatus. Is a point. That is, the reducing layer 9 and the combustion chamber 7 are arranged concentrically with the combustion chamber 7 outside and a heat transfer wall 16, and a water pipe 12 as a heat exchanger is provided in the combustion chamber 7. Water is supplied to the heat exchanger 12 to generate high-temperature and high-pressure superheated steam, and the superheated steam and the CO 2 gas 8 generated by the combustion of charcoal in the combustion chamber 7 are reduced. The point is that it is introduced into the layer 9.
  • combustion control in the oxide layer (combustion chamber) 7 is facilitated, and high temperature and high pressure that are important for the reaction mechanism of charcoal water gas generation by suitable control of the oxide layer 7. It becomes possible to generate superheated steam and facilitate its control.
  • the components of the charcoal water gas generator 1 shown in FIG. 1 are, for example, generally made of a steel plate, and the lower cylindrical portion 13 and the upper cylindrical portion 15 are bolted by a flange coupling portion 17, and each cylindrical portion is It has a heat insulation layer inside.
  • natural water tank which is not shown in figure can be provided in the water introduction part to the water pipe as a heat exchanger.
  • the superheated steam introduction means can be provided with a steam tank (not shown) as a buffer means for superheated steam pressure. Examples having these configurations (not shown) will be described later with reference to FIGS.
  • each part of the oxidation layer (combustion chamber) 7, the reduction layer 9 and the dry layer 10 is filled with charcoal, and it is confirmed that a valve (not shown) provided at the charcoal water gas outlet 14 is closed.
  • the combustion air suction port 3 is opened at start-up, and suction is performed with a suction blower (not shown) attached to the suction port.
  • ignition is performed from the positions of a plurality of (for example, six) combustion charcoal inlets / combustion air holes 4 provided around the upper portion of the oxidation layer (combustion chamber) 7.
  • an air amount adjusting shutter (not shown) provided in the combustion charcoal inlet / combustion air hole 4 is adjusted so that the entire oxidation layer (combustion chamber) 7 is measured by a temperature measuring device (not shown). After confirming that the temperature has reached a temperature (temperature display I indicated by an operation control device not shown), the combustion state is maintained.
  • the confirmation nozzle is closed, a valve (not shown) provided at the charcoal water gas outlet 14 is opened, and, for example, the charcoal water gas is sent to a fuel gas circuit in a fuel cell system to be described later.
  • the amount of air necessary for maintaining combustion and the charcoal water gas reaction is adjusted by adjusting the output of a suction high-pressure blower on the fuel cell side (not shown) and adjusting the air amount adjusting shutter.
  • the water pipe 12 provided in the combustion chamber 7, a raw water tank provided outside (not shown), and a water vapor supply function unit including a water vapor tank enter the reduction layer 9 in a high temperature atmosphere.
  • Supply high-temperature, high-pressure superheated steam Thereby, the charcoal water gas reaction shown in FIG. 8 is maintained.
  • the temperature of the superheated steam is 600 ° C., for example.
  • the temperature is set to 800 ° C., for example.
  • charcoal is burned in the oxidation layer (combustion chamber) 7 first, and the reducing layer 9 of the charcoal water gas generator 1 is maintained in a temperature zone necessary for the reaction.
  • a stable combustion state is a condition.
  • carbon dioxide (CO 2 ) generated by combustion is guided from the oxidation layer 7 to the reduction layer.
  • the charcoal filled in the reduction layer 9 is heated from the oxidation layer (combustion chamber) 7 through, for example, a concentric steel plate heat transfer wall 16, and a high-temperature reducing atmosphere is formed in the reduction layer.
  • the high-temperature and high-pressure superheated steam previously generated in the oxide layer 7 is supplied to cause the charcoal water gas reaction (C + H 2 O ⁇ CO + H 2 , C + 2H 2 O ⁇ CO 2 + 2H 2 ).
  • a shift reaction CO + H 2 O ⁇ CO 2 + H 2
  • heat is supplied through the heat transfer wall 16 to maintain a temperature zone necessary for the water gas reaction.
  • an operation control device displays the measurement value by inputting the measurement value in the temperature measurement device, and performs control for adjusting the combustion air amount so that a necessary temperature band can be maintained.
  • FIG. 4 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to an embodiment of the present invention.
  • the fuel cell is a polymer solid electrolyte type (PEFC) / phosphorus fuel using only hydrogen gas (H 2 ) as a fuel.
  • PEFC polymer solid electrolyte type
  • HP 2 hydrogen gas
  • PAFC charcoal water gas for acid type
  • the fuel cell power generation system shown in FIG. 4 includes a charcoal water gas generator 1a, a superheated steam generator 12a, a fuel cell device 20, a dust remover 21, a CO reformer 22, a gas cooler 23, a gas It comprises a filter 24 and a fuel cell off gas utilization device 26.
  • Reference numeral 25 denotes condensed water generated in the gas cooler 23.
  • the superheated steam generated in the superheated steam generator 12a is introduced into the reduction layer of the charcoal water gas generator 4 to cause a water gas reaction.
  • the charcoal water gas generator 1a and the superheated steam generator 12a are combined, and the superheated steam generated in the superheated steam generator is introduced into the reduction layer of the charcoal water gas generator to perform a water gas reaction.
  • the apparatus to be performed can be configured integrally, and the integrated apparatus is preferably the charcoal water gas production apparatus shown in FIG.
  • carbon monoxide (CO) is contained in the composition of the charcoal water gas, so that the final hydrogen content is increased by further steam reforming. It is necessary to let Therefore, the CO reformer 22 is provided.
  • carbon monoxide (CO) is removed by a process such as adsorption / re-release, but the CO reformer 22 does not remove (CO) but a superheated steam generator.
  • the reforming is performed by converting (CO) into (CO 2 ) by a shift reaction (CO + H 2 O ⁇ CO 2 + H 2 ) between superheated steam supplied from 12a to the CO reformer 22 and (CO).
  • a slow duster 21 or a gas filter 24 is provided between the charcoal water gas generator 1a and the fuel cell device 20 in order to remove dust in the gas. Further, in order to cool the charcoal water gas in accordance with the operating temperature of the fuel cell device 20, a gas cooler 23 is provided, and the energy of the residual gas (off gas) of the charcoal water gas that has not been consumed in the fuel cell device 20 is provided. In order to utilize this, a fuel cell off-gas utilization device 26 is provided.
  • FIG. 5 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to a different embodiment of the present invention.
  • the fuel cell can use both hydrogen gas (H 2 ) and carbon monoxide (CO) as fuel.
  • the system flow when using charcoal water gas for molten carbonate type (MCFC) and oxide solid electrolyte type (SOFC) is shown.
  • a gas heating device 30 is provided to heat the charcoal water gas according to the operating temperature of the fuel cell device 20.
  • the combustion heat of charcoal is necessary for (i) maintaining the charcoal water gas reaction temperature zone and (b) improving the efficiency of water gasification. It can utilize for a superheated steam generation part.
  • the control of the heat supply system with respect to the endothermic reaction is unified, the control becomes easier as compared with the conventional technique in which multiple control is performed.
  • (c) it is possible to unify heating energy sources in the fuel cell, thereby facilitating operational management and stabilizing the system.
  • the reformer heat source when city gas (13A) or the like is used in a conventional fuel cell system, the reformer heat source generally uses a city gas and a fuel cell off-gas that is fluctuating rapidly. System control becomes multi-dimensional. Compared to such a conventional method, in the case of the present invention using the charcoal water gas, the heat source for heating of each part can be unified to the combustion state control of the oxidation layer (combustion chamber) as described above, so that the control is possible. It becomes easy.
  • FIG. 6 is a diagram showing an example of a calculation result of the energy balance of the embodiment according to the charcoal water gas fuel cell power generation system of FIG.
  • FIG. 6 is a trial calculation for a phosphoric acid fuel cell (PAFC) with an output of 100 kW.
  • PAFC phosphoric acid fuel cell
  • the required amount of charcoal water gas is 90 [m 3 / h]
  • the amount of charcoal supplied is approximately 23 [kg / h].
  • the weight of the hydrogen content in the charcoal water gas 1 [m 3 ] is 53.58 g with a maximum hydrogen concentration of 60%.
  • the charcoal water gas generator 1 shown in FIG. 1 has a two-part structure in which an upper cylindrical portion and a lower cylindrical portion are flange-coupled, and the capacity of the charcoal water gas gas generator can be changed according to the output of the fuel cell.
  • a divided structure of three or more divisions can also be used.
  • positioning of the water pipe 12 as a heat exchanger can be suitably changed as needed.
  • the water pipe 12 as the heat exchanger shown in FIG. 1 is merely a steam generating means, and the superheated steam introducing means 18 or 18a shown in FIG. Reheating means may be provided to generate superheated steam.
  • the reheating means may be a charcoal combustion apparatus provided separately from the combustion chamber of FIG. 1 or another heating apparatus, for example, an induction heating apparatus using electromagnetic induction.
  • the introduction part of the superheated steam S shown in FIGS. 2 and 3 can be provided with a plurality of injection nozzles inside the ring-shaped hollow pipe.
  • FIG. 9 is a conceptual diagram of a charcoal water gas production apparatus according to an embodiment using the induction heating apparatus of the present invention
  • FIG. 10 is a charcoal water gas showing the form of a heated steam spray nozzle with respect to the embodiment of FIG. It is a composition conceptual diagram of a manufacturing device.
  • the charcoal water gas generator main body 1 in FIG. 9 is substantially the same as the charcoal water gas generator main body 1 shown in FIG. 1, but the introduction portion of the superheated steam into the reduction layer 9 is a reduction layer lower introduction portion 65a, The main difference is that the reducing layer intermediate portion introducing portion 65b and the reducing layer upper portion introducing portion 65c are arranged at three locations. Then, superheated steam heated by the induction heating device 64 is introduced into the introduction portions 65a, 65b, and 65c through the flow rate adjusting valves 44, 45, and 46, respectively, and as shown in FIG. Superheated steam is jetted into the reduction layer 9 from, for example, six superheated steam jet nozzles 66 provided in a ring shape at the introduction portion.
  • the steam generated by supplying water from the raw water tank 61 to the steam generating coil 62 serving as a heat exchanger provided in the combustion chamber 7 is supplied to the induction heating device 64.
  • Superheated steam is generated by heating by flowing.
  • 9 and 10 63 is a steam tank provided for pressure buffering, 41, 42 and 43 are flow rate adjusting valves, and 64a is a power source for the induction heating device 64.
  • a superheated steam generator “Genesis (trade name)” manufactured by Nomura Engineering Co., Ltd. can be used.
  • the reason why the superheated steam introduction part to the reducing layer 9 is arranged at three places, the lower part of the reducing layer, the middle part of the reducing layer, and the upper part of the reducing layer as described above will be described. Since the aquatic gas reaction occurs at a portion where the steam contacts the charcoal, the more the portion where the superheated steam is injected from the superheated steam injection nozzle to the reduction layer, the more the amount of generated charcoal aquatic gas is increased. Therefore, according to the embodiment of FIGS. 9 and 10, the introduction ratio of superheated steam in the introduction part of superheated steam to the reducing layer 9 according to the amount of power generation required for the fuel cell device using charcoal aquatic gas.
  • the introduction part of the superheated steam into the reduction layer may be only the lower part of the reduction layer, or when combining the lower part, the middle part, and the upper part, It is possible to use all three locations.
  • SYMBOLS 1, 1a Charcoal water gas generator, 2: Charcoal inlet upper lid part, 3: Combustion air suction port at start-up, 4: Charcoal inlet / combustion air hole, 5: Ash outlet, 6: Grid, 7: Oxidation Layer (combustion chamber), 8: CO2 gas, 9: reducing layer, 10: dry layer, 11: ash layer, 12: water pipe (heat exchanger), 12a: superheated steam generator, 13: lower cylindrical part, 14 : Charcoal water gas outlet, 15: Upper cylindrical part, 16: Heat transfer wall, 17: Flange joint, 18, 18a: Superheated steam introduction means, 20: Fuel cell power generator, 21: Dust remover, 22: CO Reformer, 23: gas cooler, 24: gas filter, 25: condensed water, 26: fuel cell off-gas utilization device, 30: gas heating device, 41 to 46: valve, 61: raw water tank, 62: steam generating coil 63: Steam tank, 64: Induction heating device, 65a

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Abstract

[Problem] To provide a charcoal syngas manufacturing method and apparatus, and a fuel cell power generation system using said manufacturing method and apparatus, which are designed to improve water gas reaction stability and gasification efficiency and to improve the controllability of operation when combined with a fuel cell. [Solution] A charcoal syngas manufacturing apparatus equipped with: an upright cylindrical charcoal syngas-generating unit (1) having a combustion chamber (7), a reducing layer (9), and a drying layer (10); and various supply means for supplying charcoal, water, and air to the charcoal syngas-generating unit. The reducing layer and the combustion chamber are disposed as concentric cylinders with the combustion chamber on the outside and a heat transfer wall (16) therebetween. A heat exchanger (12) is provided inside the combustion chamber. Water is supplied to said heat exchanger to generate high temperature/high pressure superheated water vapor, or water from a raw water tank is supplied to the heat exchanger to generate water vapor and, by heating said water vapor via an induction heating unit, superheated water vapor is generated. The water gas reaction is conducted by introducing said superheated water vapor into the reducing layer (9).

Description

木炭水性ガスの製造方法と装置、並びに同製造方法及び装置を使用した燃料電池発電システムCharcoal water gas production method and apparatus, and fuel cell power generation system using the production method and apparatus
　本発明は、木炭と水とから水性ガス反応により木炭水性ガスを製造する製造方法と装置、並びに同製造方法及び装置を使用した燃料電池発電システムに関する。 The present invention relates to a production method and apparatus for producing a charcoal water gas from charcoal and water by a water gas reaction, and a fuel cell power generation system using the production method and apparatus.
　クリーンなエネルギーとして燃料電池発電システムの実用化が進められている。燃料電池の形式には、電解質の種類、改質原料の種類等によって、高分子固体電解質型(PEFC)，リン酸型(PAFC)，熔融炭酸塩型(MCFC)，ならびに酸化物固体電解質型(SOFC)等があり、後者程、運転温度が高い。 Fuel cell power generation systems are being put to practical use as clean energy. Depending on the type of electrolyte, the type of reforming material, etc., the type of fuel cell depends on the polymer solid electrolyte type (PEFC), phosphoric acid type (PAFC), molten carbonate type (MCFC), and oxide solid electrolyte type ( SOFC), etc., and the latter has a higher operating temperature.
　例えば、運転温度が約８０℃と比較的低いタイプのPEFCは、家庭用としての分散型の利用が期待されている（特許文献１参照）。また、出力１００ｋＷ程度のPAFC（運転温度が約２００℃）は、中小規模の分散型の電源としての利用が期待されている。一方、MCFC（運転温度が約６５０～７００℃）やSOFC（運転温度が約９００～１０００℃）は、比較的高い発電効率のため、大規模な電源としての利用が期待されている。 For example, a PEFC having a relatively low operating temperature of about 80 ° C. is expected to be used in a distributed manner for home use (see Patent Document 1). In addition, PAFC with an output of about 100 kW (operating temperature is about 200 ° C.) is expected to be used as a medium- and small-scale distributed power source. On the other hand, MCFC (operating temperature is about 650 to 700 ° C.) and SOFC (operating temperature is about 900 to 1000 ° C.) are expected to be used as a large-scale power source because of relatively high power generation efficiency.
　PEFCやPAFCなどの中小規模の分散型燃料電池用の燃料ガスとしては、特許文献１にも記載されたように、従来、都市ガス（13Aガス）が一般的に使用されている。都市ガス以外に、ナフサやLPガス、さらには下水汚泥からメタン発酵処理して得られる消化ガスを利用した燃料電池も知られている（特許文献２参照）。 As described in Patent Document 1, city gas (13A gas) has been generally used as a fuel gas for small and medium-sized distributed fuel cells such as PEFC and PAFC. In addition to city gas, fuel cells using digestion gas obtained by methane fermentation from naphtha, LP gas, and sewage sludge are also known (see Patent Document 2).
　ここで、燃料ガスの成分について言及すると、上記都市ガス（13Aガス）の成分は、ガス会社により多少の差異はあるものの、一般に、メタン(CH4)89.6[%]・エタン(C2H6)5.62[%]・プロパン（C3H8)3.43［%]・ブタン(C4H10)1.35[%]とされている。また，下水汚泥由来のメタンガスにおけるメタンの濃度は約60[%]と言われている。 Here, referring to the components of the fuel gas, the components of the city gas (13A gas) are generally methane (CH 4 ) 89.6 [%] ethane (C 2 H 6 ), although there are some differences depending on the gas companies. ) 5.62 [%] Propane (C 3 H 8 ) 3.43 [%] Butane (C 4 H 10 ) 1.35 [%] The methane concentration in methane gas derived from sewage sludge is said to be about 60%.
　これらのガスを利用した燃料電池発電システムは既に実用化されているが、都市ガスを利用する場合は都市的インフラストラクチャーの普及度に左右される。また下水汚泥由来のメタンガスを利用する場合には、下水汚泥メタン発酵プラントとの併設になるので、分散用としては利用し難い面がある。また、分散型電源とし常用ならびに非常用に備えるために移動設置可能な液化石油ガス(LPG)を利用することも選択肢としては考えられているが、これも供給体制の面で制約される。そこで，地域単位で備蓄可能で持続可能なエネルギー源の調達が必要となる。 Although fuel cell power generation systems using these gases have already been put into practical use, when using city gas, it depends on the degree of urban infrastructure penetration. Moreover, when using methane gas derived from sewage sludge, it is difficult to use as a dispersion because it is combined with a sewage sludge methane fermentation plant. In addition, the use of liquefied petroleum gas (LPG) that can be moved and installed as a distributed power source for regular and emergency use is considered as an option, but this is also limited in terms of supply system. Therefore, it is necessary to procure sustainable energy sources that can be stored locally.
　前記燃料ガス以外に、木質バイオマス燃料の利用も検討されている（特許文献３参照）。
特許文献３の段落［０００３］には、バイオマス燃料を用いた発電方式として、下記が記載されている。即ち、「（１）バイオマス燃料を直接ボイラで燃焼させ、例えば、蒸気タービンにより発電する方式、（２）微生物を利用してバイオマス燃料を発酵させてメタンガスを取り出し、例えばガスエンジン、デュアルフュエルディーゼルエンジン、または燃料電池に供給して発電する方式、（３）バイオマス資源を、ガス発生炉においてガス化して可燃ガスを発生し、このガスを、例えばガスエンジンやデュアルフュエルディーゼルエンジンに供給して発電する方式等がある。」と記載されている。 In addition to the fuel gas, use of woody biomass fuel is also being studied (see Patent Document 3).
In paragraph [0003] of Patent Document 3, the following is described as a power generation method using biomass fuel. That is, “(1) A method in which biomass fuel is directly burned in a boiler, for example, power generation by a steam turbine; (2) Fermentation of biomass fuel using microorganisms to extract methane gas, for example, a gas engine, a dual fuel diesel engine (3) Biomass resources are gasified in a gas generation furnace to generate a combustible gas, and this gas is supplied to, for example, a gas engine or a dual fuel diesel engine to generate electricity. There is a system etc. ".
　また、特許文献３の段落［００１４］～［００１５］には、ガス化炉にバイオマス燃料を投入して、酸化および還元反応を用いて、CO, H2, CH4, C2H6等のガスを発生させ、この発生ガスを用いて発電することが記載されている。 Further, in paragraphs [0014] to [0015] of Patent Document 3, biomass fuel is introduced into a gasifier, and oxidation, reduction reaction, and the like are performed using CO, H 2 , CH 4 , C 2 H 6, and the like. It is described that gas is generated and power is generated using the generated gas.
　しかしながら、上記のようなバイオマス燃料を直接ガス化したガスを利用する場合には、発生ガスに含まれるタール分の処理が必要となり、この問題が、木質バイオマス燃料を利用した発電方式の実用化を妨げる大きな要因となっている。 However, when using the gas obtained by directly gasifying the biomass fuel as described above, it is necessary to treat the tar contained in the generated gas, and this problem is the practical application of the power generation system using woody biomass fuel. It has become a major factor to prevent.
　さらに、東日本大震災を経験した我が国においては、持続可能な安全でかつ取扱いの容易なエネルギー源として、歴史的に利用されてきた木炭の活用が注目されている。木炭は薪と比較してエネルギー密度が高く貯蔵ならびに流通性に優れる。さらに、持続性の点から見ても地域社会単位の歴史的な製炭業を復活させれば容易に確保できる利点があると考えられる。特にエネルギー源としての貯蔵の容易さならびに質の変動のなさは地域単位で備蓄する場合の優位性に富むと言える。 Furthermore, in Japan, which has experienced the Great East Japan Earthquake, the use of charcoal that has been used historically as a sustainable, safe and easy-to-handle energy source is attracting attention. Charcoal has a higher energy density and better storage and distribution compared to firewood. Furthermore, from the standpoint of sustainability, it is considered that there is an advantage that can be easily secured if the historical coal-making industry of the community unit is revived. In particular, the ease of storage as an energy source and the absence of quality fluctuations can be said to be advantageous in the case of stockpiling on a regional basis.
　上記木炭と水とから水性ガス反応により木炭水性ガスを製造する製造方法と装置に関しては、従来から木炭を利用した自動車(木炭バス)の歴史もありある程度完成している。
本願発明者等も、木炭水性ガスを利用して、自動車用ガソリンエンジンをガスエンジンの形で駆動し発電を行う方式を開発し実証実験を完了している。 The manufacturing method and apparatus for producing a charcoal water gas from the charcoal and water by a water gas reaction have been completed to some extent due to the history of automobiles using charcoal (charcoal bus).
The inventors of the present application have also developed a system for generating electricity by driving a gasoline engine for automobiles in the form of a gas engine using charcoal water gas, and have completed a demonstration experiment.
　この木炭の利用によれば、現代における地球規模の課題である温室効果ガス(特に、CO2)フリーとなるので、環境上のメリットも期待できる。 By using this charcoal, it becomes free of greenhouse gases (especially CO 2 ), which is a global issue today, so that environmental benefits can also be expected.
　木炭水性ガスは、木材(2C42H60O28)を製炭して得られる木炭(3C10H5O＋C30H20O3)と水(H2O)とから水性ガス反応により作られる。その組成は、水素ガス(H2)約60[%]・一酸化炭素(CO)約20[%]・残り二酸化炭素（CO2）・メタンガス（CH4）の混合ガスである。木炭水性ガスを利用する場合には、都市ガスなどを利用する時に必要な「脱硫器」を必要とせず、プロセスのシンプル化が期待できる。 The charcoal water gas is produced by a water gas reaction from charcoal (3C 10 H 5 O + C 30 H 20 O 3 ) obtained by making wood (2C 42 H 60 O 28 ) and water (H 2 O). Its composition is a mixed gas of hydrogen gas (H 2 ) of about 60 [%], carbon monoxide (CO) of about 20 [%], remaining carbon dioxide (CO 2 ), and methane gas (CH 4 ). When using charcoal water gas, the "desulfurizer" required when using city gas, etc. is not required, and simplification of the process can be expected.
　ところで、木炭の水性ガス反応は吸熱反応であり、それに必要な熱エネルギーの供給が不可欠となる。都市ガス利用の場合には、改質器において起動時には都市ガスを使い、起動後は燃料電池動作におけるオフガスを用いて熱エネルギーの供給を行う。この方式の場合、両ガスの発熱量に大きな差異があること、ならびに構造上同一バーナーで燃焼させることが必要であり、その安定性確保に高度な制御技術が必要となる。これに対して、木炭水性ガス反応の場合には、木炭(固体)と水とから木炭水性ガスを作るので、吸熱反応に必要な熱エネルギーは木炭の一部を燃焼させることで容易に確保できる。またその燃焼に関する制御も目視可能とすることで容易となる。 By the way, the water gas reaction of charcoal is an endothermic reaction, and it is essential to supply the necessary heat energy. In the case of using city gas, city gas is used at the time of start-up in the reformer, and heat energy is supplied using off-gas in the fuel cell operation after start-up. In the case of this method, there is a large difference in the calorific values of both gases, and it is necessary to burn with the same burner because of the structure, and advanced control technology is required to ensure its stability. On the other hand, in the case of charcoal water gas reaction, charcoal water gas is made from charcoal (solid) and water, so the heat energy required for endothermic reaction can be easily secured by burning a part of charcoal. . Further, the control regarding the combustion is facilitated by making it visible.
　従来の木炭水性ガス発生装置の概略構成および木炭水性ガス発生の反応形態を説明する図を、図７および図８に示す。従来の装置は、一般に、酸化層（以下、燃焼室ともいう。
）、還元層、乾燥層とから構成された縦型木炭水性ガス発生装置の前記酸化層の下方に、外部から水を供給することにより、木炭水性ガスを発生するように構成されている。図７、図８に基づいて、装置の構成および木炭水性ガス発生の反応形態について詳述する。 FIGS. 7 and 8 show a schematic configuration of a conventional charcoal water gas generator and a reaction form of charcoal water gas generation. Conventional devices generally have an oxide layer (hereinafter also referred to as a combustion chamber).
), A vertical charcoal water gas generator composed of a reducing layer and a dry layer is configured to generate charcoal water gas by supplying water from the outside below the oxide layer. Based on FIG. 7, FIG. 8, the structure of an apparatus and the reaction form of charcoal water gas generation | occurrence | production are explained in full detail.
　図７に示す縦型木炭水性ガス発生装置５１は、木炭充填部５２と、その下方に設けた火格子５３と、木炭充填部５２の上方から木炭水性ガスＧを取出すための取出装置５８とからなる。前記木炭充填部５２は後述する図８に示すように、酸化層（燃焼室）７ａと、還元層９ａと、乾燥層１０ａとからからなる。なお、火格子５３の下方は、燃焼した木炭の灰層１１ａである。 A vertical charcoal water gas generator 51 shown in FIG. 7 includes a charcoal filling part 52, a grate 53 provided below the charcoal filling part 52, and a take-out device 58 for taking out the charcoal water gas G from above the charcoal filling part 52. Become. As shown in FIG. 8 described later, the charcoal filling section 52 includes an oxidation layer (combustion chamber) 7a, a reduction layer 9a, and a dry layer 10a. Below the grate 53 is a burned charcoal ash layer 11a.
　さらに、図７に示すように、木炭水性ガス発生装置５１の下方には、焚き口５４と、燃焼室の点検口５５と、燃焼室の側壁を包囲する耐火材５６とが設けられ、上方には、木炭水性ガスの発生を確認するためのガス点検トーチ５７が設けられている。また、前記取出装置５８には、ガス内のダストを除去するためのフィルター６０が設けられている。このフィルター６０は、例えば、コークス層と金タワシ等の層とからなる。 Further, as shown in FIG. 7, a burning port 54, a combustion chamber inspection port 55, and a refractory material 56 surrounding the combustion chamber side wall are provided below the charcoal water gas generator 51, and Is provided with a gas inspection torch 57 for confirming the generation of charcoal water gas. The take-out device 58 is provided with a filter 60 for removing dust in the gas. The filter 60 includes, for example, a coke layer and a layer such as a gold scrubber.
　そして、木炭水性ガスＧを発生するためには、装置下方に、燃焼用の空気Ａと水Ｗとを供給する。そして、木炭の燃焼熱により水を加熱し、水蒸気とされた水と木炭との水性ガス反応によって、木炭充填部５２の主として還元層９ａにおいてＨ2・ＣＯガス主体の木炭水性ガスを発生し、乾燥層１０ａを経由して、前記取出装置５８から木炭水性ガスＧを取出す。 And in order to generate | occur | produce the charcoal water gas G, the combustion air A and the water W are supplied below an apparatus. Then, the water is heated by the combustion heat of the charcoal, and by the water gas reaction between the water and the charcoal, the charcoal filling gas 52 mainly generates the H 2 · CO gas-based charcoal water gas in the reduction layer 9a, The charcoal water gas G is taken out from the take-out device 58 via the dry layer 10a.
　上記装置の運転の際、各部の温度帯域は酸化層７ａは約900～1300℃，還元層９ａは800～900℃，乾燥層１０ａは600～800℃に維持されるように酸化層７ａの燃焼度合いを制御する。なお、燃焼は酸化層下部の焚き口５４に適当な燃焼副材を投入後着火し開始する。着火後内部の温度条件が確立し木炭水性ガスが発生したことを、ガス点検トーチ部５７における着火により確認する。 During the operation of the above apparatus, the combustion of the oxide layer 7a is performed so that the temperature zone of each part is maintained at about 900 to 1300 ° C for the oxide layer 7a, 800 to 900 ° C for the reduction layer 9a, and 600 to 800 ° C for the dry layer 10a. Control the degree. Combustion is started by igniting a suitable combustion auxiliary material in the outlet 54 below the oxide layer. After the ignition, it is confirmed by ignition in the gas inspection torch portion 57 that the internal temperature condition is established and the charcoal water gas is generated.
　ガス発生の安定状態を確認後は、燃焼に必要な理論空気量ならびに内部温度条件を維持する。各層間で木炭由来の炭素と燃焼用空気ならびに水(水蒸気)により生じる化学反応は、図８に示す通りと言われている。この結果、木炭水性ガス発生装置で水素ガス(H2)ならびに一酸化炭素(CO)主体の混合ガスが作られる。 After confirming the stable state of gas generation, maintain the theoretical air volume and internal temperature conditions required for combustion. It is said that a chemical reaction caused by carbon derived from charcoal, combustion air, and water (water vapor) between the respective layers is as shown in FIG. As a result, a mixed gas mainly composed of hydrogen gas (H 2 ) and carbon monoxide (CO) is produced by the charcoal water gas generator.
　次に、図８について詳述する。図８は、塩ノ谷幸造著「木炭自動車」（1996年、株式会社パワー社発行）を参考にして作成したものである。前述の酸化層７ａ、還元層９ａ、乾燥層１０ａ、灰層１１ａを左側に模式的に示し、その右側には各層における化学反応を示す。 Next, FIG. 8 will be described in detail. FIG. 8 is created with reference to Kozo Shionoya's “Charcoal Vehicle” (published by Power Corporation in 1996). The aforementioned oxide layer 7a, reduction layer 9a, dry layer 10a, and ash layer 11a are schematically shown on the left side, and the chemical reaction in each layer is shown on the right side.
　酸化層７ａでは、Ｃ＋Ｏ2→ＣＯ2（炭素の完全燃焼）および２Ｃ＋Ｏ2→２ＣＯ（炭素の不完全燃焼）が行われ、燃焼熱を発生する。 In the oxide layer 7a, C + O 2 → CO 2 (complete combustion of carbon) and 2C + O 2 → 2CO (incomplete combustion of carbon) are performed to generate combustion heat.
　還元層９ａでは、Ｃ＋ＣＯ2→２ＣＯ（還元反応）、Ｃ＋Ｈ2Ｏ→ＣＯ＋Ｈ2およびＣ＋２Ｈ2Ｏ→ＣＯ2＋２Ｈ2（水性ガス反応）、ＣＯ＋Ｈ2Ｏ→ＣＯ2＋Ｈ2（シフト反応）、ならびに、ＣＯ＋３Ｈ2→ＣＨ4＋Ｈ2ＯおよびＣ＋２Ｈ2→ＣＨ4の反応が行われる。なお、上記５つの反応の内、還元反応および水性ガス反応は吸熱反応であるので、反応を適正に行うためには、熱供給が必要であり、この熱供給は、酸化層７ａにおける燃焼熱によって行われる。 In the reducing layer 9a, C + CO 2 → 2CO (reduction reaction), C + H 2 O → CO + H 2 and C + 2H 2 O → CO 2 + 2H 2 (water gas reaction), CO + H 2 O → CO 2 + H 2 (shift reaction), and Reactions of CO + 3H 2 → CH 4 + H 2 O and C + 2H 2 → CH 4 are performed. Of the above five reactions, the reduction reaction and the water gas reaction are endothermic reactions. Therefore, in order to perform the reaction properly, heat supply is required, and this heat supply is caused by the combustion heat in the oxide layer 7a. Done.
　従って、木炭水性ガスとしては、Ｈ2・ＣＯガス主体で、その他ＣＯ2・ＣＨ4を含む混合ガスとなる。その組成は前述のように、水素ガス(H2)約60[%]・一酸化炭素(CO)約20[%]・残り二酸化炭素（CO2）・メタンガス（CH4）の混合ガスである。 Therefore, the charcoal water gas is a mixed gas mainly containing H 2 · CO gas and containing CO 2 · CH 4 . As described above, the composition is a mixed gas of hydrogen gas (H 2 ) approximately 60 [%], carbon monoxide (CO) approximately 20 [%], the remaining carbon dioxide (CO 2 ), and methane gas (CH 4 ). .
　ところで、上述したような従来の木炭水性ガス製造装置によって木炭水性ガスを製造する場合、水性ガス反応の安定性やガス化効率が十分ではなく、また、燃料電池と組み合わせた場合の運転制御性にも難がある等の問題がある。その理由は下記のとおりである。 By the way, when producing charcoal water gas by the conventional charcoal water gas production apparatus as described above, the stability and gasification efficiency of the water gas reaction are not sufficient, and the operation controllability when combined with a fuel cell is achieved. There are also problems such as difficulties. The reason is as follows.
　上記従来の装置の場合、木炭水性ガスを発生する際に、装置下方に水Ｗを滴下して水蒸気を発生し、その水蒸気を還元層に導入するようにしているので、水蒸気が燃焼用の空気Ａに乗って飛散し、還元層への水蒸気の導入制御が適正にできない。即ち、木炭水性ガス反応温度帯域維持の安定的制御ができない。また、酸化層（燃焼室）における燃焼の制御も適正にできない。従って、水性ガス反応の安定性やガス化効率が低下する。また、上記の不適正は、燃料電池における燃料ガスの供給にも影響を及ぼし、燃料電池の運転制御性にも問題が生ずる。 In the case of the above conventional apparatus, when the charcoal water gas is generated, water W is dropped at the lower part of the apparatus to generate water vapor, and the water vapor is introduced into the reducing layer. It is scattered on A and the introduction control of water vapor into the reducing layer cannot be properly performed. That is, the stable control of maintaining the charcoal water gas reaction temperature zone cannot be performed. Also, the combustion control in the oxide layer (combustion chamber) cannot be properly performed. Accordingly, the stability of the water gas reaction and the gasification efficiency are lowered. In addition, the above-mentioned improperness also affects the supply of fuel gas in the fuel cell, causing problems in the operation controllability of the fuel cell.
　一方、特許文献４には、上記木炭水性ガスを製造する製造方法と装置に関する改良技術が記載されている。また、木炭水性ガスを発電装置に利用することも記載されている。 On the other hand, Patent Document 4 describes an improved technique related to a production method and apparatus for producing the above charcoal water gas. It also describes the use of charcoal water gas for power generation devices.
　特許文献４は、その要約や段落［００１４］の記載から明かなように、「化石燃料を全く消費しないで炭化処理すること、および炭化温度の制御性を高めるとともに高温炭化の制御性を高めることを目的として、炭化炉２内もしくは別置きのガス化炉内で、木炭が８００℃～１２００℃に高温化した段階において空気および水蒸気と接触させてガス化反応を起こさせて多量の可燃ガスを含む木炭ガスを製造し、この木炭ガスを燃焼ガス発生供給手段３にて燃焼させて得られる燃焼ガスで被処理物を加熱して炭化処理を行うこと」を開示している。また、「この木炭ガスを使用して発電手段１２にてガス発電を行い、得られた電力で炭化処理システムの機器を運転する。」ことも開示している。 As is apparent from the summary and the description of paragraph [0014], Patent Document 4 states that “carbonization without consuming fossil fuel at all, and that the controllability of the carbonization temperature and the controllability of high-temperature carbonization are improved. For the purpose of, in the carbonization furnace 2 or in a separate gasification furnace, when the charcoal is heated to a temperature of 800 ° C to 1200 ° C, it is brought into contact with air and water vapor to cause a gasification reaction to generate a large amount of combustible gas. It is disclosed that a charcoal gas is produced, and the object to be treated is heated by a combustion gas obtained by burning the charcoal gas in the combustion gas generation and supply means 3 to perform carbonization treatment. Moreover, it discloses that "this charcoal gas is used to perform gas power generation by the power generation means 12, and the carbonization processing system equipment is operated with the obtained electric power."
　さらに、特許文献４は図１又は図２の実施例において、「炭化炉２又はガス化炉１０において発生した木炭ガスにより、熱交換器を介して水を加熱して水蒸気を発生し、この水蒸気を炭化炉２の上部又はガス化炉１０の下部に導入することにより、木炭水性ガス反応を行うこと」も開示している。 Further, Patent Document 4 describes in the embodiment of FIG. 1 or FIG. 2 that “the charcoal gas generated in the carbonization furnace 2 or the gasification furnace 10 generates water vapor by heating water through a heat exchanger. Is introduced into the upper part of the carbonization furnace 2 or the lower part of the gasification furnace 10 to perform a charcoal water gas reaction ".
　しかしながら、特許文献４に記載された製造方法と装置によっても、下記のように、水性ガス反応の安定性やガス化効率が十分ではなく、燃料電池と組み合わせた場合の運転制御性にも問題がある。 However, even with the manufacturing method and apparatus described in Patent Document 4, the stability and gasification efficiency of the water gas reaction are not sufficient as described below, and there is a problem in the operation controllability when combined with a fuel cell. is there.
　即ち、特許文献４に記載された方式の場合、後述する本願発明と比較して、木炭水性ガス反応のための熱供給系の制御が多元的となるので、木炭水性ガス反応温度帯域維持の安定的制御ができず、また、燃料電池と組み合わせた場合の運転制御性にも難がある。詳細は後述する本願発明の説明によって理解される。 That is, in the case of the method described in Patent Document 4, since the control of the heat supply system for the charcoal water gas reaction becomes multi-dimensional as compared with the present invention described later, the stability of the charcoal water gas reaction temperature zone maintenance is stable. Control is not possible, and operation controllability when combined with a fuel cell is difficult. Details will be understood from the following description of the present invention.
特開２００２－１２４２８８号公報JP 2002-124288 A 特開平１１－１２６６２９号公報Japanese Patent Laid-Open No. 11-126629 特開２００６－８３２９３号公報JP 2006-83293 A 特開２００３－２５３２７８号公報JP 2003-253278 A
　本発明は上記の点に鑑みなされたものであり、その目的は、水性ガス反応の安定性やガス化効率の向上を図り、また、燃料電池と組み合わせた場合の運転制御性の向上を図った木炭水性ガス製造方法と装置、並びに同製造方法及び装置を使用した燃料電池発電システムを提供することにある。 The present invention has been made in view of the above points, and its purpose is to improve the stability of the water gas reaction and the gasification efficiency, and to improve the operation controllability when combined with a fuel cell. A charcoal water gas production method and apparatus, and a fuel cell power generation system using the production method and apparatus.
　前記目的を達成するために、本発明によれば、酸化層（燃焼室）と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置を用いて、木炭と水とから水性ガス反応により木炭水性ガスを製造する方法において、
　前記還元層と燃焼室とを、燃焼室を外側とし伝熱壁を介して同心円筒状に配設し、かつ前記燃焼室内に熱交換器を設け、この熱交換器に水を供給して高温・高圧の過熱水蒸気を発生し、この過熱水蒸気を前記還元層に導入することによって前記水性ガス反応を行わせることとする。 In order to achieve the above object, according to the present invention, a vertical cylindrical charcoal water gas generator having an oxidation layer (combustion chamber), a reduction layer, and a dry layer, and charcoal, water, and air are supplied to the charcoal water. In a method for producing a charcoal water gas by a water gas reaction from charcoal and water using a charcoal water gas production device comprising each supply means for supplying to the gas generator,
The reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, and a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to increase the temperature. The high-temperature superheated steam is generated, and the water gas reaction is performed by introducing the superheated steam into the reduction layer.
　また、前記過熱水蒸気の温度は、使用する木炭に応じて異なった温度とすることが好ましい。その理由は、還元層の温度帯域（800～900℃）において、水性ガス反応度ならびに水性ガスシフト反応度が、精煉度・孔の面積などの木炭の性質により変動するので、反応を適正に制御するためには、使用する木炭の性質に応じて、過熱水蒸気の温度を異なった温度とすることが好ましいからである。 Also, the temperature of the superheated steam is preferably different depending on the charcoal used. The reason for this is that the water gas reactivity and water gas shift reactivity fluctuate depending on charcoal properties such as refinement and pore area in the temperature zone of the reducing layer (800-900 ° C), so the reaction is controlled appropriately. This is because it is preferable to set the temperature of the superheated steam to a different temperature depending on the nature of the charcoal used.
　さらに、前記目的を達成するための木炭水性ガス製造装置としては、本発明によれば、燃焼室と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置において、
　前記還元層と燃焼室とを、燃焼室を外側とし伝熱壁を介して同心円筒状に配設し、前記燃焼室内に熱交換器を設け、この熱交換器に水を供給して高温・高圧の過熱水蒸気を発生するようにし、かつ、前記過熱水蒸気と、前記燃焼室において木炭の燃焼により発生したＣＯ2ガスとを、前記還元層に導入するようにしてなり、さらに、前記燃焼室は前記伝熱壁と下部円筒形部とにより形成し、前記還元層は前記伝熱壁と上部円筒形部とにより形成し、前記乾燥層は上部円筒形部により形成し、前記上部円筒形部には木炭水性ガス取出し口と木炭水性ガス発生装置の起動時燃焼空気吸引口とを設け、前記下部円筒形部には木炭投入口兼燃焼空気導入口を設け、かつ前記上部円筒形部の上蓋部には、木炭投入口を設けるものとする。 Furthermore, as a charcoal water gas production apparatus for achieving the above object, according to the present invention, a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer, and a dry layer, charcoal, water, and In the charcoal water gas production apparatus comprising each supply means for supplying air to the charcoal water gas generator,
The reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to High pressure superheated steam is generated, and the superheated steam and CO 2 gas generated by the combustion of charcoal in the combustion chamber are introduced into the reduction layer, and the combustion chamber is The heat transfer wall and the lower cylindrical part are formed, the reduction layer is formed by the heat transfer wall and the upper cylindrical part, and the dry layer is formed by the upper cylindrical part, and the upper cylindrical part is formed on the upper cylindrical part. Is provided with a charcoal water gas outlet and a combustion air suction port at the start of the charcoal water gas generator, the lower cylindrical part is provided with a charcoal inlet and combustion air inlet, and the upper lid part of the upper cylindrical part Shall be provided with a charcoal inlet.
　また、前記発明の実施態様としては、前記燃焼室内に設ける熱交換器は、前記下部円筒形部の筒の内部に管を螺旋状に巻回したものとし、前記管内に水を通流してなるものとすることが、熱交換器の構成をシンプルとする観点から好ましい。 Further, as an embodiment of the invention, the heat exchanger provided in the combustion chamber is formed by spirally winding a tube inside the cylinder of the lower cylindrical portion, and water is passed through the tube. From the viewpoint of simplifying the configuration of the heat exchanger, it is preferable.
　さらに、前記同心円筒状に配設した前記還元層および燃焼室の下方には格子を設け、この格子の隙間から、前記木炭の燃焼により発生したＣＯ2ガスを前記還元層へ導入し、かつこの格子の下方に、燃焼に伴って発生する灰を排出するようにすることが好ましい。 Furthermore, a lattice is provided below the reducing layer and the combustion chamber arranged in the concentric cylindrical shape, and CO 2 gas generated by combustion of the charcoal is introduced into the reducing layer through a gap between the lattice, and this It is preferable to discharge ash generated with combustion below the grid.
　また、前記過熱水蒸気の前記還元層への導入は、前記還元層の下方から前記格子を貫通して行うようにするか、あるいは、前記還元層の上方から前記上蓋部および乾燥層を貫通して行うようにすることが好ましい。 In addition, the superheated steam is introduced into the reduction layer through the lattice from below the reduction layer, or through the upper lid and the dry layer from above the reduction layer. It is preferable to do so.
　そして、前記目的を達成するための燃料電池発電システムの発明としては下記を特徴とする。即ち、燃焼室と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置と、前記燃焼室において発生した木炭の燃焼熱により水を過熱して、高温・高圧の過熱水蒸気を発生するようにした過熱水蒸気発生器と、前記木炭水性ガス製造装置において生成した木炭水性ガスを燃料ガスとして供給して発電する燃料電池装置とを備える木炭水性ガス式燃料電池発電システムであって、
　前記過熱水蒸気発生器において発生した過熱水蒸気を前記木炭水性ガス発生装置が有する還元層へ導入して水性ガス反応を行わせるようにすることを特徴とする。 The invention of the fuel cell power generation system for achieving the above object is characterized as follows. Namely, a charcoal water gas production comprising a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer and a dry layer, and each supply means for supplying charcoal, water and air to the charcoal water gas generator. Apparatus, a superheated steam generator that superheats water by combustion heat of charcoal generated in the combustion chamber to generate high-temperature and high-pressure superheated steam, and a charcoal water gas generated in the charcoal water gas production apparatus A charcoal water gas fuel cell power generation system comprising a fuel cell device that generates electricity by supplying a fuel gas as a fuel gas,
The superheated steam generated in the superheated steam generator is introduced into a reduction layer of the charcoal water gas generator so as to cause a water gas reaction.
　また、前記発明の実施態様としては、前記木炭水性ガス発生装置と過熱水蒸気発生器とを組合せ、かつ、前記過熱水蒸気発生器において発生した過熱水蒸気を前記木炭水性ガス発生装置が有する還元層へ導入して水性ガス反応を行わせるようにする装置は一体化して構成した木炭水性ガス製造装置とし、この一体化して構成した装置は、前述した木炭水性ガス製造装置のいずれか一つに記載の装置とすることを特徴とする。 Further, as an embodiment of the invention, the charcoal water gas generator and the superheated steam generator are combined, and superheated steam generated in the superheated steam generator is introduced into the reduction layer of the charcoal water gas generator. The apparatus for causing the water gas reaction to be performed is an integrated charcoal water gas production apparatus, and the integrated apparatus is an apparatus according to any one of the aforementioned charcoal water gas production apparatuses. It is characterized by.
　さらに、前記木炭水性ガス発生装置と前記燃料電池装置との間に、前記木炭水性ガスに含有するＣＯを改質するＣＯ改質機を設け、このＣＯ改質機に、前記過熱水蒸気発生器において発生した過熱水蒸気を供給して、ＣＯをＣＯ2にシフトするシフト反応を行わせるようにすることが好ましい。燃料電池が前記PEFCやPAFCなどの場合には、燃料ガス内にＣＯを含むことは、電極触媒劣化の観点から好ましくないので、前記シフト反応を行わせるようにすることが好ましい。 Further, a CO reformer for reforming CO contained in the charcoal water gas is provided between the charcoal water gas generator and the fuel cell device, and the CO reformer is provided with the superheated steam generator. It is preferable to supply the generated superheated steam so that a shift reaction for shifting CO to CO 2 is performed. When the fuel cell is a PEFC, PAFC, or the like, it is not preferable to include CO in the fuel gas from the viewpoint of deterioration of the electrode catalyst. Therefore, the shift reaction is preferably performed.
　また、前記木炭水性ガス発生装置と前記燃料電池装置との間に、前記燃料電池装置の運転温度に応じて前記木炭水性ガスを冷却または加熱するガス冷却器またはガス加熱装置を設けることが好ましい。燃料電池が、前記PEFCやPAFCなどの場合にはガス冷却器を必要とし、MCFCやSOFC、特にSOFCの場合にはガス加熱装置を必要とする。 Further, it is preferable that a gas cooler or a gas heating device for cooling or heating the charcoal water gas is provided between the charcoal water gas generator and the fuel cell device according to the operating temperature of the fuel cell device. When the fuel cell is the PEFC or PAFC, a gas cooler is required, and when the fuel cell is an MCFC or SOFC, particularly a SOFC, a gas heating device is required.
　さらに、前記木炭水性ガス発生装置と前記燃料電池装置との間に、ガス内のダストを除去するために、徐塵機またはガスフィルタを設けることが好ましい。 Further, it is preferable to provide a gradual duster or a gas filter between the charcoal water gas generator and the fuel cell device in order to remove dust in the gas.
　さらにまた、前記燃料電池装置において消費されなかった木炭水性ガスの残ガス（オフガス）のエネルギーを活用するための燃料電池オフガス利用装置を備えることが、省エネの観点から好ましい。 Furthermore, it is preferable from the viewpoint of energy saving to provide a fuel cell off-gas utilization device for utilizing the energy of the residual gas (off gas) of the charcoal water gas that has not been consumed in the fuel cell device.
　上記の木炭水性ガス製造方法の発明によれば、木炭水性ガス反応（吸熱反応）のための熱供給を、燃焼室において発生する燃焼熱の伝熱壁を介しての熱伝達や、燃焼排ガスや過熱水蒸気が有する熱などにより行うので、適正かつ安定した熱供給が実現可能であり、かつ熱供給の制御が一元的となるので、従来技術に比較して木炭水性ガス反応温度帯域維持の安定的制御ができる。その結果、木炭水性ガス発生の熱効率が向上すると共に、後に詳述するように、燃料電池と組み合わせた場合の運転制御性の向上を図ることができる。 According to the invention of the method for producing charcoal water gas, heat supply for the charcoal water gas reaction (endothermic reaction) can be performed by heat transfer through a heat transfer wall of combustion heat generated in the combustion chamber, combustion exhaust gas, Because it uses the heat of superheated steam, etc., it is possible to achieve an appropriate and stable heat supply, and the control of the heat supply will be unified, so the charcoal water gas reaction temperature zone can be maintained more stably than in the prior art. Can control. As a result, the thermal efficiency of the charcoal water gas generation is improved, and as described later in detail, the operation controllability when combined with the fuel cell can be improved.
　また、上記の木炭水性ガス製造装置の発明によれば、シンプルな構成により上記の製造方法が実施でき、また、制御性も良好となる。 Further, according to the invention of the apparatus for producing charcoal water gas, the above production method can be carried out with a simple configuration, and the controllability is also improved.
　さらに、上記の燃料電池発電システムの発明によれば、燃料電池の燃料ガスとして木炭水性ガスを利用するので、従来の燃料電池発電システム、即ち、都市ガス、下水汚泥由来のメタンガス、木質バイオマス燃料等を利用したシステムに比較して、背景技術の項で記載したような利点を有する。また、上記の木炭水性ガス製造装置と組み合わせることにより、効率の向上および運転制御性の向上を図ることができる。 Furthermore, according to the above fuel cell power generation system invention, since the charcoal water gas is used as the fuel gas of the fuel cell, the conventional fuel cell power generation system, that is, city gas, sewage sludge-derived methane gas, woody biomass fuel, etc. Compared to a system using the above, there are advantages as described in the background section. Further, by combining with the above-described charcoal water gas production apparatus, it is possible to improve efficiency and improve operation controllability.
　木炭水性ガスを利用した燃料電池発電システムは、従来実施されていないシステムである。そこで、前述の記載と一部重複するものの、あらためて、木炭水性ガス式燃料電池発電システムの技術的かつ社会的優位性についてまとめて列記すると、以下のとおりである。
（１）木炭水性ガスの利用によれば温室効果ガス(特に、CO2)フリーとなり、また、燃料電池からの排出物は水のみとなるので、環境上のメリットが大きい。
（２）低騒音化が容易に実現できるので電力需要先に近接設置可能であり、かつ、地域の分散型エネルギー設備として多様化も可能であり、社会的利用メリットが大きい。
（３）設備全体のコンパクト化が可能である。
（４）設備全体の制御性が良く、かつ取扱いが容易である。
（５）従来のバイオマス燃料を直接ガス化したガスを利用する場合と比較して、発生ガスに含まれるタール分の処理が不要のためメンテナンス性が良く、かつ、高効率である。
（６）間伐材の利用促進により林地の適正化を図ることができ、森林の修復に貢献できる社会的メリットがある。 A fuel cell power generation system using charcoal water gas has not been implemented conventionally. Therefore, although partially overlapping with the above description, the technical and social superiority of the charcoal water gas fuel cell power generation system is listed as follows.
(1) The use of charcoal water gas makes the greenhouse gas (especially CO 2 ) free, and the only waste from the fuel cell is water.
(2) Since noise reduction can be easily realized, it can be installed close to the power demand destination and can be diversified as a distributed energy facility in the region, which has a great merit for social use.
(3) The entire facility can be made compact.
(4) Good controllability of the entire equipment and easy handling.
(5) Compared to the case where a gas obtained by directly gasifying a conventional biomass fuel is used, it is not necessary to treat the tar contained in the generated gas, so that the maintainability is good and the efficiency is high.
(6) Forest land can be optimized by promoting the use of thinned wood, and there is a social merit that can contribute to forest restoration.
本発明の実施形態による木炭水性ガス製造装置の模式断面図。The schematic cross section of the charcoal water gas manufacturing apparatus by embodiment of this invention. 本発明の実施例による木炭水性ガス製造装置の側断面図。The sectional side view of the charcoal water gas manufacturing apparatus by the Example of this invention. 本発明の異なる実施例による木炭水性ガス製造装置の側断面図。The sectional side view of the charcoal water gas manufacturing apparatus by the Example from which this invention differs. 本発明の実施形態による木炭水性ガス式燃料電池発電システムの概略系統図。1 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to an embodiment of the present invention. 本発明の異なる実施形態による木炭水性ガス式燃料電池発電システムの概略系統図。1 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to a different embodiment of the present invention. 図４の木炭水性ガス式燃料電池発電システムに係る実施例のエネルギー収支の試算結果の一例を示す図The figure which shows an example of the calculation result of the energy balance of the Example which concerns on the charcoal water gas type fuel cell power generation system of FIG. 従来の木炭水性ガス発生装置の概略構成を示す図The figure which shows schematic structure of the conventional charcoal water gas generator. 従来の木炭水性ガス発生装置における木炭水性ガス発生の反応形態の説明図Explanatory drawing of reaction form of charcoal water gas generation in conventional charcoal water gas generator 本発明の誘導加熱装置を用いた実施例による木炭水性ガス製造装置の構成概念図。BRIEF DESCRIPTION OF THE DRAWINGS The block conceptual diagram of the charcoal water gas manufacturing apparatus by the Example using the induction heating apparatus of this invention. 図９の実施例に関し加熱水蒸気噴射ノズルの形態を示した木炭水性ガス製造装置の構成概念図。The structure conceptual diagram of the charcoal water-gas manufacturing apparatus which showed the form of the heating steam injection nozzle regarding the Example of FIG.
　以下、この発明による実施の形態について、図１～６、９および１０に示す実施例に基づいて説明する。なお、前記図１～６、９および１０において、機能が同一の対応部材には同一符号を付して、それらの重複説明を省略する。 Hereinafter, embodiments according to the present invention will be described based on examples shown in FIGS. 1 to 6, 9 and 10. 1 to 6, 9 and 10, corresponding members having the same function are denoted by the same reference numerals, and redundant description thereof is omitted.
　図１は本発明の実施形態による木炭水性ガス製造装置の模式断面図であり、図２は、本発明の実施例による木炭水性ガス製造装置の側断面図であり、図３は、本発明の異なる実施例による木炭水性ガス製造装置の側断面図である。 FIG. 1 is a schematic cross-sectional view of a charcoal water gas production apparatus according to an embodiment of the present invention, FIG. 2 is a side cross-sectional view of a charcoal water gas production apparatus according to an embodiment of the present invention, and FIG. It is a sectional side view of the charcoal water gas manufacturing apparatus by a different Example.
　図１に示す木炭水性ガス製造装置は、木炭水性ガス発生装置１と、図示しない木炭、水および空気を前記ガス発生装置へ供給する各供給手段と、温度計測装置および運転制御装置と、ならびに過熱水蒸気導入手段（図２，３には図示）とからなる。 The charcoal water gas production apparatus shown in FIG. 1 includes a charcoal water gas generator 1, supply means (not shown) for supplying charcoal, water, and air to the gas generator, a temperature measurement device and an operation control device, and an overheat It consists of water vapor introducing means (shown in FIGS. 2 and 3).
　前記木炭水性ガス発生装置１は、木炭投入口上蓋部２、起動時燃焼空気吸引口３、木炭投入口兼燃焼空気孔４、灰排出口５、格子６、酸化層（燃焼室）７、還元層９、乾燥層１０、灰層１１、熱交換器としての水管１２、下部円筒形部１３、木炭水性ガス取出し口１４、上部円筒形部１５、伝熱壁１６、下部円筒形部１３と上部円筒形部１５とのフランジ結合部１７を備える。 The charcoal water gas generator 1 includes a charcoal inlet top lid 2, a combustion air suction port 3 at startup, a charcoal inlet / combustion air hole 4, an ash outlet 5, a grid 6, an oxide layer (combustion chamber) 7, a reduction Layer 9, dry layer 10, ash layer 11, water pipe 12 as heat exchanger, lower cylindrical part 13, charcoal water gas outlet 14, upper cylindrical part 15, heat transfer wall 16, lower cylindrical part 13 and upper part A flange coupling part 17 with the cylindrical part 15 is provided.
　図２～３に示す実施例は、上記図１に係る木炭水性ガス製造装置の実施例であり、一部の記載を省略または追加した図である。図２の実施例は、熱交換器としての水管１２において生成した過熱水蒸気を還元層９の下方から前記格子６を貫通して導入するようにしてなる過熱水蒸気導入手段１８を備えた実施例であり、図３は還元層９の上方から前記上蓋部２および乾燥層１０を貫通して導入するようにしてなる過熱水蒸気導入手段１８ａを備えた実施例である。構造上の観点からは上方から導入する方が簡便で有利であるが、熱ロスの観点からは下方から導入する方が有利である。なお、導入された過熱水蒸気Ｓは、木炭水性ガス取出し口１４から流出するガスの吸引作用により、過熱水蒸気Ｓの導入部から上方へ流れて拡散する。 The embodiment shown in FIGS. 2 to 3 is an embodiment of the apparatus for producing charcoal water gas according to FIG. 1, and a part of the description is omitted or added. The embodiment of FIG. 2 is an embodiment provided with superheated steam introduction means 18 configured to introduce superheated steam generated in a water pipe 12 as a heat exchanger through the lattice 6 from below the reducing layer 9. FIG. 3 shows an embodiment provided with superheated steam introducing means 18a which is introduced through the upper lid portion 2 and the dry layer 10 from above the reducing layer 9. From the viewpoint of structure, introduction from above is simple and advantageous, but from the viewpoint of heat loss, introduction from below is advantageous. The introduced superheated steam S flows upward from the introduction portion of the superheated steam S and diffuses by the suction action of the gas flowing out from the charcoal water gas outlet 14.
　図１に示す木炭水性ガス発生装置１と、図７に示した従来の木炭水性ガス発生装置５１との基本的な相違は酸化層と還元層の配置関係であり、従来の装置は酸化層と還元層とが円筒状に垂直方向上下に配設されているのに対し、本発明に係る図１に示す木炭水性ガス発生装置１の場合には、装置の下方に同心円筒状に配設した点である。即ち、前記還元層９と燃焼室７とを、燃焼室７を外側とし伝熱壁１６を介して同心円筒状に配設し、前記燃焼室７内に熱交換器としての水管１２を設け、この熱交換器１２に水を供給して高温・高圧の過熱水蒸気を発生するようにし、かつ、この過熱水蒸気と、前記燃焼室７において木炭の燃焼により発生したＣＯ2ガス８とを、前記還元層９に導入するようにした点である。 The fundamental difference between the charcoal water gas generator 1 shown in FIG. 1 and the conventional charcoal water gas generator 51 shown in FIG. 7 is the arrangement relationship of the oxidation layer and the reduction layer. Whereas the reducing layer is arranged vertically in the vertical direction, in the case of the charcoal water gas generator 1 shown in FIG. 1 according to the present invention, it is arranged concentrically below the apparatus. Is a point. That is, the reducing layer 9 and the combustion chamber 7 are arranged concentrically with the combustion chamber 7 outside and a heat transfer wall 16, and a water pipe 12 as a heat exchanger is provided in the combustion chamber 7. Water is supplied to the heat exchanger 12 to generate high-temperature and high-pressure superheated steam, and the superheated steam and the CO 2 gas 8 generated by the combustion of charcoal in the combustion chamber 7 are reduced. The point is that it is introduced into the layer 9.
　この構成により、本発明によれば、酸化層（燃焼室）７における燃焼制御が容易となり、また、酸化層７の好適な制御により、木炭水性ガス発生の反応メカニズム上、重要となる高温・高圧の過熱蒸気を発生させ、その制御も容易にすることが可能となる。 With this configuration, according to the present invention, combustion control in the oxide layer (combustion chamber) 7 is facilitated, and high temperature and high pressure that are important for the reaction mechanism of charcoal water gas generation by suitable control of the oxide layer 7. It becomes possible to generate superheated steam and facilitate its control.
　なお、図１に示す木炭水性ガス発生装置１の構成部材は、例えば、概ね鋼板製で、下部円筒形部１３および上部円筒形部１５はフランジ結合部１７でボルト結合され、各円筒形部は、その内方に断熱層を備えている。また、熱交換器としての水管への水導入部には、図示しない原水タンクを設けることができる。さらに、過熱水蒸気導入手段には、過熱水蒸気圧力の緩衝手段として図示しない水蒸気タンクを設けることもできる。これらの図示しない構成を有する実施例については、図９および１０に基づいて後述する。 The components of the charcoal water gas generator 1 shown in FIG. 1 are, for example, generally made of a steel plate, and the lower cylindrical portion 13 and the upper cylindrical portion 15 are bolted by a flange coupling portion 17, and each cylindrical portion is It has a heat insulation layer inside. Moreover, the raw | natural water tank which is not shown in figure can be provided in the water introduction part to the water pipe as a heat exchanger. Further, the superheated steam introduction means can be provided with a steam tank (not shown) as a buffer means for superheated steam pressure. Examples having these configurations (not shown) will be described later with reference to FIGS.
　次に、木炭水性ガス製造装置の運転方法について述べる。 Next, the operation method of the charcoal water gas production apparatus will be described.
　まず、酸化層（燃焼室）７、還元層９および乾燥層１０の各部に木炭を充填し、木炭水性ガス取出し口１４に設けた図示しないバルブが、閉の状態であることを確認する。 First, each part of the oxidation layer (combustion chamber) 7, the reduction layer 9 and the dry layer 10 is filled with charcoal, and it is confirmed that a valve (not shown) provided at the charcoal water gas outlet 14 is closed.
　続いて、起動時燃焼空気吸引口３を開とし，同吸引口に装着する図示しない吸引ブロアで吸引する。燃焼用空気を吸引しつつ、酸化層（燃焼室）７上部周辺に設けた複数個（例えば６個）の燃焼用木炭投入口兼燃焼用空気孔４の位置から着火する。着火後は、燃焼用木炭投入口兼燃焼用空気孔４に設けた図示しない空気量調節用シャッターを調節し、酸化層（燃焼室）７全体が、図示しない温度計測装置によって計測された所定の温度（図示しない運転制御装置が示す温度表示Ｉ）に達した状態を確認後、その燃焼状態を維持する。 Subsequently, the combustion air suction port 3 is opened at start-up, and suction is performed with a suction blower (not shown) attached to the suction port. While the combustion air is sucked, ignition is performed from the positions of a plurality of (for example, six) combustion charcoal inlets / combustion air holes 4 provided around the upper portion of the oxidation layer (combustion chamber) 7. After ignition, an air amount adjusting shutter (not shown) provided in the combustion charcoal inlet / combustion air hole 4 is adjusted so that the entire oxidation layer (combustion chamber) 7 is measured by a temperature measuring device (not shown). After confirming that the temperature has reached a temperature (temperature display I indicated by an operation control device not shown), the combustion state is maintained.
　酸化層（燃焼室）７の燃焼状態安定後、酸化層の外周に設けた伝熱壁１６を介し伝達される燃焼熱ならびに格子６経由で還元層９に流入する燃焼排ガス（ＣＯ2ガス）８により還元層９内の木炭が加熱される。還元層９内の温度が所定の温度（図示しない運転制御装置が示す温度表示ＩＩ）に達した後、木炭水性ガスの発生状況を、木炭水性ガス取出し口１４に併設する図示しないガス点検トーチに設けた確認用ノズルを開とし、ガスに着火し確認する。この場合、前記燃焼用空気の吸引ブロアは停止し前記起動時燃焼空気吸引口３は閉にしてから行なう。 After the combustion state of the oxide layer (combustion chamber) 7 is stabilized, the combustion heat transmitted through the heat transfer wall 16 provided on the outer periphery of the oxide layer and the combustion exhaust gas (CO 2 gas) 8 flowing into the reduction layer 9 via the lattice 6 As a result, the charcoal in the reducing layer 9 is heated. After the temperature in the reducing layer 9 reaches a predetermined temperature (temperature display II indicated by an operation controller (not shown)), the generation state of the charcoal water gas is indicated on a gas inspection torch (not shown) attached to the charcoal water gas outlet 14. Open the confirmation nozzle provided and ignite the gas for confirmation. In this case, the combustion air suction blower is stopped and the start-up combustion air suction port 3 is closed.
　その後、前記確認用ノズルを閉とし、木炭水性ガス取出し口１４に設けた図示しないバルブを開にして、例えば、後述する燃料電池システムにおける燃料ガスの回路に木炭水性ガスを送る。この状態において燃焼ならびに木炭水性ガス反応を維持するために必要な空気量の調整は、図示しない燃料電池側の吸引高圧ブロワーの出力調整と、前記空気量調節用シャッターの調節とにより行う。 Thereafter, the confirmation nozzle is closed, a valve (not shown) provided at the charcoal water gas outlet 14 is opened, and, for example, the charcoal water gas is sent to a fuel gas circuit in a fuel cell system to be described later. In this state, the amount of air necessary for maintaining combustion and the charcoal water gas reaction is adjusted by adjusting the output of a suction high-pressure blower on the fuel cell side (not shown) and adjusting the air amount adjusting shutter.
　燃焼状態ならびに還元層内の温度の安定を確認後、燃焼室７に設けた水管１２、図示しない外部に設けた原水タンクならびに水蒸気タンクからなる水蒸気供給機能部により、高温雰囲気の還元層９内に、高温・高圧の過熱水蒸気を供給する。これにより、図８に示した木炭水性ガス反応が維持される。過熱水蒸気の温度は、例えば、６００℃である。なお、使用する木炭の性質によっては、例えば、８００℃とする。 After confirming the combustion state and the stability of the temperature in the reduction layer, the water pipe 12 provided in the combustion chamber 7, a raw water tank provided outside (not shown), and a water vapor supply function unit including a water vapor tank enter the reduction layer 9 in a high temperature atmosphere. Supply high-temperature, high-pressure superheated steam. Thereby, the charcoal water gas reaction shown in FIG. 8 is maintained. The temperature of the superheated steam is 600 ° C., for example. Depending on the nature of the charcoal used, the temperature is set to 800 ° C., for example.
　木炭水性ガス発生装置１内での各種の反応については、図８に示した通りである。まず、第一に酸化層(燃焼室)７で木炭を燃焼し、木炭水性ガス発生装置１の還元層９を反応に必要な温度帯域に維持する。そのためには燃焼状態の安定が条件となる。加えて、還元層９での還元反応（C＋CO2→2CO）を安定させるために燃焼で生じた二酸化炭素(CO2)を有効に利用すべく酸化層７から還元層に誘導する。 Various reactions in the charcoal water gas generator 1 are as shown in FIG. First, charcoal is burned in the oxidation layer (combustion chamber) 7 first, and the reducing layer 9 of the charcoal water gas generator 1 is maintained in a temperature zone necessary for the reaction. For this purpose, a stable combustion state is a condition. In addition, in order to stabilize the reduction reaction (C + CO 2 → 2CO) in the reduction layer 9, carbon dioxide (CO 2 ) generated by combustion is guided from the oxidation layer 7 to the reduction layer.
　次に酸化層(燃焼室)７から例えば同心円状の鋼板製伝熱壁１６を介して、還元層９に充填された木炭が加熱され、還元層内は高温の還元雰囲気となる。この状態で、先に酸化層７で発生した高温・高圧の過熱水蒸気を供給することにより、木炭水性ガス反応（C＋H2O→CO＋H2，C＋2H2O→CO2＋2H2）を生じさせる。さらに、還元層９内ではシフト反応(CO＋H2O →CO2＋H2)が起こる。これらの還元反応，水性ガス反応は吸熱反応であるので、前記伝熱壁１６を介して熱供給を行い、水性ガス反応に必要な温度帯域を維持する。 Next, the charcoal filled in the reduction layer 9 is heated from the oxidation layer (combustion chamber) 7 through, for example, a concentric steel plate heat transfer wall 16, and a high-temperature reducing atmosphere is formed in the reduction layer. In this state, the high-temperature and high-pressure superheated steam previously generated in the oxide layer 7 is supplied to cause the charcoal water gas reaction (C + H 2 O → CO + H 2 , C + 2H 2 O → CO 2 + 2H 2 ). Further, a shift reaction (CO + H 2 O → CO 2 + H 2 ) occurs in the reducing layer 9. Since these reduction reaction and water gas reaction are endothermic reactions, heat is supplied through the heat transfer wall 16 to maintain a temperature zone necessary for the water gas reaction.
　なお、図１に示す木炭水性ガス製造装置に設ける図示しない温度計測装置は、少なくとも、酸化層（燃焼室）７および還元層９にそれぞれ設け、必要に応じて、その他の部分に設けることもできる。また、図示しない運転制御装置は、温度計測装置における計測値の入力によってその計測値を表示すると共に、必要な温度帯域が維持できるように、燃焼空気量の調整操作を行うための制御を行う。 1 is provided at least in the oxidation layer (combustion chamber) 7 and the reduction layer 9, and may be provided in other portions as necessary. . Further, an operation control device (not shown) displays the measurement value by inputting the measurement value in the temperature measurement device, and performs control for adjusting the combustion air amount so that a necessary temperature band can be maintained.
　水性ガス反応，還元反応，シフト反応で作られる木炭水性ガスの組成は、前述のように一般に、水素ガス(H2)約60[%]，一酸化炭素(CO)約20[%]，残り(二酸化炭素CO2・メタンCH4)といわれている。この一酸化炭素(CO)ならびに水素ガス(H2)主体の木炭水性ガスを燃料電池の燃料に使う場合、燃料電池の形式によっては、一酸化炭素(CO)の分離・改質を必要とする。 Water gas reaction, the composition of the reduction reaction, charcoal water gas produced in the shift reaction, generally as described above hydrogen gas (H 2) of about 60 [%], carbon monoxide (CO) 20 [%], the remaining It is said to be (carbon dioxide CO 2 / methane CH 4 ). When carbon monoxide (CO) and hydrogen gas (H 2 ) -based charcoal water gas is used as fuel for fuel cells, depending on the type of fuel cell, separation and reforming of carbon monoxide (CO) may be required. .
　次に、木炭水性ガスを燃料ガスとして利用する燃料電池発電システムについて述べる。 Next, a fuel cell power generation system using charcoal water gas as fuel gas will be described.
　図４は、本発明の実施形態による木炭水性ガス式燃料電池発電システムの概略系統図であり、燃料電池が、水素ガス(H2)のみを燃料とする高分子固体電解質型(PEFC)・リン酸型(PAFC)に木炭水性ガスを利用する場合のシステムフローを示す。 FIG. 4 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to an embodiment of the present invention. The fuel cell is a polymer solid electrolyte type (PEFC) / phosphorus fuel using only hydrogen gas (H 2 ) as a fuel. The system flow when using charcoal water gas for acid type (PAFC) is shown.
　図４に示す燃料電池発電システムは、木炭水性ガス発生装置１ａと、過熱水蒸気発生器１２ａと、燃料電池装置２０と、除塵機２１と、ＣＯ改質機２２と、ガス冷却器２３と、ガスフィルタ２４と、燃料電池オフガス利用装置２６とからなる。なお、２５はガス冷却器２３において発生した凝縮水を示す。 The fuel cell power generation system shown in FIG. 4 includes a charcoal water gas generator 1a, a superheated steam generator 12a, a fuel cell device 20, a dust remover 21, a CO reformer 22, a gas cooler 23, a gas It comprises a filter 24 and a fuel cell off gas utilization device 26. Reference numeral 25 denotes condensed water generated in the gas cooler 23.
　そして、上記システムにおいては、前記過熱水蒸気発生器１２ａにおいて発生した過熱水蒸気を前記木炭水性ガス発生装置４が有する還元層へ導入して水性ガス反応を行わせるようにする。 In the above system, the superheated steam generated in the superheated steam generator 12a is introduced into the reduction layer of the charcoal water gas generator 4 to cause a water gas reaction.
　なお、前記木炭水性ガス発生装置１ａと過熱水蒸気発生器１２ａとを組合せ、かつ、前記過熱水蒸気発生器において発生した過熱水蒸気を前記木炭水性ガス発生装置が有する還元層へ導入して水性ガス反応を行わせるようにする装置は一体化して構成することができ、この一体化して構成した装置は、前記図１に示した木炭水性ガス製造装置とすることが好ましい。 The charcoal water gas generator 1a and the superheated steam generator 12a are combined, and the superheated steam generated in the superheated steam generator is introduced into the reduction layer of the charcoal water gas generator to perform a water gas reaction. The apparatus to be performed can be configured integrally, and the integrated apparatus is preferably the charcoal water gas production apparatus shown in FIG.
　図４に示すシステムにおける燃料電池が前記PEFCおよびPAFCの場合、木炭水性ガスの組成中に一酸化炭素(CO)が約20%含まれるので、さらに水蒸気改質を行い最終的な水素含量を増大させる必要がある。そのため、前記ＣＯ改質機２２を設ける。従来技術によれば、一酸化炭素(CO)を吸着・再放出などのプロセスにより除去しているが、前記ＣＯ改質機２２においては、(CO)を除去するのではなく、過熱水蒸気発生器１２ａからＣＯ改質機２２に供給する過熱水蒸気と(CO)とのシフト反応（CO＋H2O→CO2＋H2）により、(CO)を(CO2)化することにより改質する。 When the fuel cell in the system shown in FIG. 4 is the above-mentioned PEFC and PAFC, carbon monoxide (CO) is contained in the composition of the charcoal water gas, so that the final hydrogen content is increased by further steam reforming. It is necessary to let Therefore, the CO reformer 22 is provided. According to the prior art, carbon monoxide (CO) is removed by a process such as adsorption / re-release, but the CO reformer 22 does not remove (CO) but a superheated steam generator. The reforming is performed by converting (CO) into (CO 2 ) by a shift reaction (CO + H 2 O → CO 2 + H 2 ) between superheated steam supplied from 12a to the CO reformer 22 and (CO).
　図４に示すシステムにおいては、木炭水性ガス発生装置１ａと燃料電池装置２０との間に、ガス内のダストを除去するために、徐塵機２１またはガスフィルタ２４を設けている。また、燃料電池装置２０の運転温度に応じて木炭水性ガスを冷却するために、ガス冷却器２３を設け、さらに、燃料電池装置２０において消費されなかった木炭水性ガスの残ガス（オフガス）のエネルギーを活用するために、燃料電池オフガス利用装置２６を設けている。 In the system shown in FIG. 4, a slow duster 21 or a gas filter 24 is provided between the charcoal water gas generator 1a and the fuel cell device 20 in order to remove dust in the gas. Further, in order to cool the charcoal water gas in accordance with the operating temperature of the fuel cell device 20, a gas cooler 23 is provided, and the energy of the residual gas (off gas) of the charcoal water gas that has not been consumed in the fuel cell device 20 is provided. In order to utilize this, a fuel cell off-gas utilization device 26 is provided.
　前記PEFCならびにPAFCにおいて、従来より一般的に行なわれている都市ガス(13A)を使用する場合には、ガス中に含まれる硫黄分を除去するために脱硫器が必要であり、また、下水汚泥や畜産廃棄物由来のメタンを利用する場合には、前処理装置で硫化水素(H2S)・シロキサ(R3SiO-(R2SiO)n-SiR3)・アンモニア(NH3)を除去する必要がある。木炭水性ガスを利用する場合には、その必要性がなく、システムがシンプル化すると同時に、除去に伴い発生する硫化水素などの有害物処理の必要性もなく、設備全体の維持管理が容易となる。 In the above-mentioned PEFC and PAFC, when using city gas (13A) that has been generally used conventionally, a desulfurizer is required to remove sulfur contained in the gas, and sewage sludge is used. When using methane derived from livestock and livestock waste, remove hydrogen sulfide (H 2 S), siloxa (R 3 SiO- (R 2 SiO) n-SiR 3 ), and ammonia (NH 3 ) with pretreatment equipment. There is a need to. When using charcoal water gas, there is no need for it, the system is simplified, and at the same time, there is no need for treatment of harmful substances such as hydrogen sulfide generated by the removal, and maintenance and management of the entire facility becomes easy. .
　次に図５について述べる。図５は、本発明の異なる実施形態による木炭水性ガス式燃料電池発電システムの概略系統図であり、燃料電池が、水素ガス(H2)と一酸化炭素(CO)双方を燃料として使可能な溶融炭酸塩型(MCFC)ならびに酸化物固体電解質型(SOFC)に木炭水性ガスを利用する場合のシステムフローを示す。 Next, FIG. 5 will be described. FIG. 5 is a schematic system diagram of a charcoal water gas fuel cell power generation system according to a different embodiment of the present invention. The fuel cell can use both hydrogen gas (H 2 ) and carbon monoxide (CO) as fuel. The system flow when using charcoal water gas for molten carbonate type (MCFC) and oxide solid electrolyte type (SOFC) is shown.
　図５に示すシステムの場合、一般的に都市ガス(13A)を使用する時必要とする脱硫器ならびに下水汚泥や畜産廃棄物由来のメタンを利用する場合不可欠とされている前処理装置の必要性がないことに加え、一酸化炭素(CO)改質機も必要としない。従って、システムが極めてシンプルとなり、設備の維持管理も一層容易となる。 In the case of the system shown in FIG. 5, there is a need for a desulfurizer generally required when using city gas (13A) and a pretreatment device that is indispensable when using methane from sewage sludge and livestock waste. In addition, there is no need for a carbon monoxide (CO) reformer. Therefore, the system becomes extremely simple, and the maintenance and management of the facility becomes easier.
　図５に示すシステムの場合、燃料電池の運転温度が比較的高いので、燃料電池装置２０の運転温度に応じて木炭水性ガスを加熱するためにガス加熱装置３０を設けている。 In the case of the system shown in FIG. 5, since the operating temperature of the fuel cell is relatively high, a gas heating device 30 is provided to heat the charcoal water gas according to the operating temperature of the fuel cell device 20.
　図５に示すシステムによれば、図４に示すシステムと同様に、木炭の燃焼熱を、(イ)木炭水性ガス反応温度帯域維持や、(ロ)水性ガス化の効率向上のために必要な過熱水蒸気発生部に利用することができる。その際、吸熱反応に対する熱供給系の制御が一元的であるので、多元的制御となる従来技術に比較して制御が容易となる。さらに、(ハ)燃料電池における加熱のエネルギー源を一元化でき、運転管理の容易さと系の安定化を図ることができる。 According to the system shown in FIG. 5, as in the system shown in FIG. 4, the combustion heat of charcoal is necessary for (i) maintaining the charcoal water gas reaction temperature zone and (b) improving the efficiency of water gasification. It can utilize for a superheated steam generation part. At that time, since the control of the heat supply system with respect to the endothermic reaction is unified, the control becomes easier as compared with the conventional technique in which multiple control is performed. Furthermore, (c) it is possible to unify heating energy sources in the fuel cell, thereby facilitating operational management and stabilizing the system.
　特に、従来の燃料電池システムにおいて都市ガス(13A)などを利用する場合、改質器用熱源を、都市ガスと、変動の激しい燃料電池オフガスとを利用する方式が一般的であるので、この場合、系の制御が多元的になる。このような従来の方式に比較して、木炭水性ガスを利用する本発明の場合には、上述の通り各部の加熱用熱源を酸化層（燃焼室）の燃焼状態制御に一元化できるので、制御が容易となる。 In particular, when city gas (13A) or the like is used in a conventional fuel cell system, the reformer heat source generally uses a city gas and a fuel cell off-gas that is fluctuating rapidly. System control becomes multi-dimensional. Compared to such a conventional method, in the case of the present invention using the charcoal water gas, the heat source for heating of each part can be unified to the combustion state control of the oxidation layer (combustion chamber) as described above, so that the control is possible. It becomes easy.
　次に、図６について述べる。図６は図４の木炭水性ガス式燃料電池発電システムに係る実施例のエネルギー収支の試算結果の一例を示す図である。 Next, FIG. 6 will be described. FIG. 6 is a diagram showing an example of a calculation result of the energy balance of the embodiment according to the charcoal water gas fuel cell power generation system of FIG.
　図６は、出力１００ｋＷのリン酸型燃料電池(PAFC)を対象として試算したもので、この場合、必要な木炭水性ガス量は、９０［ｍ3／ｈ］であり、木炭供給量は、約２３［ｋｇ／ｈ］となる。ここで、木炭水性ガス１［ｍ3］中の水素分の重量は、水素濃度最大６０％として、５３．５８ｇである。 FIG. 6 is a trial calculation for a phosphoric acid fuel cell (PAFC) with an output of 100 kW. In this case, the required amount of charcoal water gas is 90 [m 3 / h], and the amount of charcoal supplied is approximately 23 [kg / h]. Here, the weight of the hydrogen content in the charcoal water gas 1 [m 3 ] is 53.58 g with a maximum hydrogen concentration of 60%.
　以上、図１～図６に基づいて、本発明の基本的な実施形態を説明したが、本発明は上記の実施形態または実施例に限定されるものではなく、本発明の技術思想の範囲内において、適宜、変更が可能である。 The basic embodiment of the present invention has been described above with reference to FIGS. 1 to 6. However, the present invention is not limited to the above-described embodiment or examples, and is within the scope of the technical idea of the present invention. However, it can be changed as appropriate.
　例えば、図１に示す木炭水性ガス発生装置１は、上部円筒形部および下部円筒形部をフランジ結合した２分割構造であるが、燃料電池の出力に応じて木炭水性ガスガス発生装置の容量を可変とできるようにすべく、３分割以上の分割構造とすることもできる。また、熱交換器としての水管１２の構成や配置は、必要に応じて適宜変更可能である。 For example, the charcoal water gas generator 1 shown in FIG. 1 has a two-part structure in which an upper cylindrical portion and a lower cylindrical portion are flange-coupled, and the capacity of the charcoal water gas gas generator can be changed according to the output of the fuel cell. In order to be able to do so, a divided structure of three or more divisions can also be used. Moreover, the structure and arrangement | positioning of the water pipe 12 as a heat exchanger can be suitably changed as needed.
　さらに、図１～３の実施形態の変形として、図１に示す熱交換器としての水管１２は単なる水蒸気発生手段とし、図２または３に示す過熱水蒸気導入手段１８または１８ａに水蒸気を再加熱する再加熱手段を設けて過熱水蒸気を発生するようにすることもできる。前記再加熱手段としては、図１の燃焼室とは別に設けた木炭の燃焼装置とすることや、別の加熱装置、例えば、電磁誘導を用いた誘導加熱装置とすることもできる。 Further, as a modification of the embodiment of FIGS. 1 to 3, the water pipe 12 as the heat exchanger shown in FIG. 1 is merely a steam generating means, and the superheated steam introducing means 18 or 18a shown in FIG. Reheating means may be provided to generate superheated steam. The reheating means may be a charcoal combustion apparatus provided separately from the combustion chamber of FIG. 1 or another heating apparatus, for example, an induction heating apparatus using electromagnetic induction.
　また、図２，３に示す過熱水蒸気Ｓの導入部は、複数個の噴射ノズルをリング状中空配管のリング内方に設けたものとすることができる。 Moreover, the introduction part of the superheated steam S shown in FIGS. 2 and 3 can be provided with a plurality of injection nozzles inside the ring-shaped hollow pipe.
　次に、過熱水蒸気発生手段として誘導加熱装置を用いた異なる実施例や、過熱水蒸気の導入部に噴射ノズルを設けた実施例について、図９および１０に基づいて述べる。 Next, a different embodiment using an induction heating device as superheated steam generation means and an embodiment in which an injection nozzle is provided in the superheated steam introduction section will be described with reference to FIGS.
　図９は、本発明の誘導加熱装置を用いた実施例による木炭水性ガス製造装置の構成概念図であり、図１０は、図９の実施例に関し加熱水蒸気噴射ノズルの形態を示した木炭水性ガス製造装置の構成概念図である。 FIG. 9 is a conceptual diagram of a charcoal water gas production apparatus according to an embodiment using the induction heating apparatus of the present invention, and FIG. 10 is a charcoal water gas showing the form of a heated steam spray nozzle with respect to the embodiment of FIG. It is a composition conceptual diagram of a manufacturing device.
　図９における木炭水性ガス発生装置本体１は、図１に示す木炭水性ガス発生装置本体１と略同一であるが、過熱水蒸気の還元層９への導入部は、還元層下部用導入部６５ａ、還元層中間部用導入部６５ｂ、還元層上部用導入部６５ｃの３か所に配設している点が主に異なる。
　そして、前記導入部６５ａ、６５ｂ、６５ｃに対して、それぞれ流量調節用のバルブ４４、４５、４６を介して誘導加熱装置６４によって加熱された過熱水蒸気が導入され、図１０に示すように、前記導入部にリング状に設けた例えば６個の過熱水蒸気噴射ノズル６６から、還元層９へ過熱水蒸気が噴射される。なお、かならずしも、噴射ノズルをリング状に複数個設ける必要はなく、棒状で縦長の導入部に複数個設けることもできる。
　また、図９および１０に示す実施例においては、燃焼室７内に設けた熱交換器としての水蒸気発生コイル６２に原水タンク６１から水を供給して発生した水蒸気を、前記誘導加熱装置６４に通流して加熱することにより過熱水蒸気を発生する。
　なお、図９および１０において、６３は圧力緩衝用に設けた水蒸気タンク、４１，４２，４３は流量調節用のバルブ、６４ａは誘導加熱装置６４用の電源である。誘導加熱装置としては、例えば、野村技工株式会社製の過熱蒸気発生装置「Genesis（商品名）」を用いることができる。 The charcoal water gas generator main body 1 in FIG. 9 is substantially the same as the charcoal water gas generator main body 1 shown in FIG. 1, but the introduction portion of the superheated steam into the reduction layer 9 is a reduction layer lower introduction portion 65a, The main difference is that the reducing layer intermediate portion introducing portion 65b and the reducing layer upper portion introducing portion 65c are arranged at three locations.
Then, superheated steam heated by the induction heating device 64 is introduced into the introduction portions 65a, 65b, and 65c through the flow rate adjusting valves 44, 45, and 46, respectively, and as shown in FIG. Superheated steam is jetted into the reduction layer 9 from, for example, six superheated steam jet nozzles 66 provided in a ring shape at the introduction portion. Note that it is not always necessary to provide a plurality of injection nozzles in a ring shape, and a plurality of injection nozzles can be provided in a vertically long introduction portion.
9 and 10, the steam generated by supplying water from the raw water tank 61 to the steam generating coil 62 serving as a heat exchanger provided in the combustion chamber 7 is supplied to the induction heating device 64. Superheated steam is generated by heating by flowing.
9 and 10, 63 is a steam tank provided for pressure buffering, 41, 42 and 43 are flow rate adjusting valves, and 64a is a power source for the induction heating device 64. As the induction heating device, for example, a superheated steam generator “Genesis (trade name)” manufactured by Nomura Engineering Co., Ltd. can be used.
　次に、前述のように過熱水蒸気の還元層９への導入部を、還元層下部、還元層中間部および還元層上部の３か所に配設する理由について述べる。
　前記水生ガス反応は、木炭に水蒸気が接触した部分で起きるので、過熱水蒸気噴射ノズルから還元層へ過熱水蒸気が噴射される部分が多い程、木炭水生ガスの発生量が増大する。従って、前記図９および１０の実施例によれば、木炭水生ガスを利用する燃料電池装置が必要とされる発電量に応じて、過熱水蒸気の還元層９への導入部における過熱水蒸気の導入割合を、噴射ノズルの位置や各噴射ノズルにおける噴射量の調節によって、位置的および量的に制御することができる。
　なお、対象とするシステムによっては、前記過熱水蒸気の還元層への導入部は、還元層下部のみでよい場合もあるし、また、下部、中間部、上部の２か所を組合せる場合や、３か所全てを用いる場合があり得る。 Next, the reason why the superheated steam introduction part to the reducing layer 9 is arranged at three places, the lower part of the reducing layer, the middle part of the reducing layer, and the upper part of the reducing layer as described above will be described.
Since the aquatic gas reaction occurs at a portion where the steam contacts the charcoal, the more the portion where the superheated steam is injected from the superheated steam injection nozzle to the reduction layer, the more the amount of generated charcoal aquatic gas is increased. Therefore, according to the embodiment of FIGS. 9 and 10, the introduction ratio of superheated steam in the introduction part of superheated steam to the reducing layer 9 according to the amount of power generation required for the fuel cell device using charcoal aquatic gas. Can be controlled in a positional and quantitative manner by adjusting the position of the injection nozzle and the injection amount of each injection nozzle.
Depending on the target system, the introduction part of the superheated steam into the reduction layer may be only the lower part of the reduction layer, or when combining the lower part, the middle part, and the upper part, It is possible to use all three locations.
　なお、過熱水蒸気発生手段として、前記誘導加熱装置に代えて、木炭燃焼装置を用いることも可能である。 In addition, it is also possible to use a charcoal combustion device as the superheated steam generation means instead of the induction heating device.
　１、１ａ：木炭水性ガス発生装置、２：木炭投入口上蓋部、３：起動時燃焼空気吸引口、４：木炭投入口兼燃焼空気孔、５：灰排出口、６：格子、７：酸化層（燃焼室）、８：ＣＯ２ガス、９：還元層、１０：乾燥層、１１：灰層、１２：水管（熱交換器）、１２ａ：過熱水蒸気発生器、１３：下部円筒形部、１４：木炭水性ガス取出し口、１５：上部円筒形部、１６：伝熱壁、１７：フランジ結合部、１８、１８ａ：過熱水蒸気導入手段、２０：燃料電池発電装置、２１：除塵機、２２：ＣＯ改質機、２３：ガス冷却器、２４：ガスフィルタ、２５：凝縮水、２６：燃料電池オフガス利用装置、３０：ガス加熱装置、４１～４６：バルブ、６１：原水タンク、６２：水蒸気発生コイル、６３：水蒸気タンク、６４：誘導加熱装置、６５ａ：還元層下部用導入部、６５ｂ：還元層中間部用導入部、６５ｃ：還元層上部用導入部、６６：過熱水蒸気噴射ノズル。 DESCRIPTION OF SYMBOLS 1, 1a: Charcoal water gas generator, 2: Charcoal inlet upper lid part, 3: Combustion air suction port at start-up, 4: Charcoal inlet / combustion air hole, 5: Ash outlet, 6: Grid, 7: Oxidation Layer (combustion chamber), 8: CO2 gas, 9: reducing layer, 10: dry layer, 11: ash layer, 12: water pipe (heat exchanger), 12a: superheated steam generator, 13: lower cylindrical part, 14 : Charcoal water gas outlet, 15: Upper cylindrical part, 16: Heat transfer wall, 17: Flange joint, 18, 18a: Superheated steam introduction means, 20: Fuel cell power generator, 21: Dust remover, 22: CO Reformer, 23: gas cooler, 24: gas filter, 25: condensed water, 26: fuel cell off-gas utilization device, 30: gas heating device, 41 to 46: valve, 61: raw water tank, 62: steam generating coil 63: Steam tank, 64: Induction heating device, 65a Reducing layer lower for the introduction, 65b: introduction portion for reducing layer intermediate portion, 65c: reducing layer upper for introducing portion, 66: superheated steam jet nozzle.

Claims (16)

  1. 　酸化層（以下、燃焼室という。）と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置を用いて、木炭と水とから水性ガス反応により木炭水性ガスを製造する方法において、
    　前記還元層と燃焼室とを、燃焼室を外側とし伝熱壁を介して同心円筒状に配設し、かつ前記燃焼室内に熱交換器を設け、この熱交換器に水を供給して高温・高圧の過熱水蒸気を発生し、この過熱水蒸気を前記還元層に導入することによって前記水性ガス反応を行わせることを特徴とする木炭水性ガス製造方法。     A vertical cylindrical charcoal water gas generator having an oxide layer (hereinafter referred to as a combustion chamber), a reducing layer, and a dry layer; and each supply means for supplying charcoal, water and air to the charcoal water gas generator In a method for producing a charcoal water gas by a water gas reaction from charcoal and water using a charcoal water gas production apparatus comprising:
    The reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, and a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to increase the temperature. A method for producing a charcoal water gas comprising generating high-pressure superheated steam and introducing the superheated steam into the reducing layer to cause the water gas reaction.
  2. 　前記過熱水蒸気の温度は、使用する木炭に応じて異なった温度とすることを特徴とする請求項１に記載の製造方法。 The manufacturing method according to claim 1, wherein the temperature of the superheated steam is different depending on charcoal to be used.
  3. 　燃焼室と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置において、
    　前記還元層と燃焼室とを、燃焼室を外側とし伝熱壁を介して同心円筒状に配設し、前記燃焼室内に熱交換器を設け、この熱交換器に水を供給して高温・高圧の過熱水蒸気を発生するようにし、かつ、前記過熱水蒸気と、前記燃焼室において木炭の燃焼により発生したＣＯ2ガスとを、前記還元層に導入するようにしてなり、
    　さらに、前記燃焼室は前記伝熱壁と下部円筒形部とにより形成し、前記還元層は前記伝熱壁と上部円筒形部とにより形成し、前記乾燥層は上部円筒形部により形成し、前記上部円筒形部には木炭水性ガス取出し口と木炭水性ガス発生装置の起動時燃焼空気吸引口とを設け、前記下部円筒形部には木炭投入口兼燃焼空気導入口を設け、かつ前記上部円筒形部の上蓋部には、木炭投入口を設けることを特徴とする木炭水性ガス製造装置。     In a charcoal water gas production apparatus comprising: a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer, and a dry layer; and each supply means for supplying charcoal, water, and air to the charcoal water gas generator ,
    The reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, a heat exchanger is provided in the combustion chamber, and water is supplied to the heat exchanger to High pressure superheated steam is generated, and the superheated steam and CO 2 gas generated by combustion of charcoal in the combustion chamber are introduced into the reduction layer,
    Further, the combustion chamber is formed by the heat transfer wall and the lower cylindrical portion, the reduction layer is formed by the heat transfer wall and the upper cylindrical portion, and the dry layer is formed by the upper cylindrical portion, The upper cylindrical part is provided with a charcoal water gas outlet and a combustion air suction port at the start of the charcoal water gas generator, the lower cylindrical part is provided with a charcoal inlet and a combustion air inlet, and the upper part An apparatus for producing a charcoal water gas, characterized in that a charcoal inlet is provided in the upper lid of the cylindrical part.
  4. 　前記燃焼室内に設ける熱交換器は、前記下部円筒形部の筒の内部に管を螺旋状に巻回したものとし、前記管内に水を通流してなるものとすることを特徴とする請求項３に記載の装置。 The heat exchanger provided in the combustion chamber is configured such that a pipe is spirally wound inside a cylinder of the lower cylindrical portion, and water is passed through the pipe. 3. The apparatus according to 3.
  5. 　前記同心円筒状に配設した前記還元層および燃焼室の下方には格子を設け、この格子の隙間から、前記木炭の燃焼により発生したＣＯ2ガスを前記還元層へ導入し、かつこの格子の下方に、燃焼に伴って発生する灰を排出するようにすることを特徴とする請求項３に記載の装置。 A grid is provided below the reduction layer and the combustion chamber arranged in the concentric cylinder shape, and CO 2 gas generated by the combustion of the charcoal is introduced into the reduction layer from a gap between the grids. 4. The apparatus according to claim 3, wherein ash generated by combustion is discharged downward.
  6. 　前記過熱水蒸気の前記還元層への導入は、前記還元層の下方から前記格子を貫通して行うようにしてなることを特徴とする請求項５に記載の装置。 6. The apparatus according to claim 5, wherein the superheated steam is introduced into the reduction layer through the lattice from below the reduction layer.
  7. 　前記過熱水蒸気の前記還元層への導入は、前記還元層の上方から前記上蓋部および乾燥層を貫通して行うようにすることを特徴とする請求項１に記載の装置。 The apparatus according to claim 1, wherein the superheated steam is introduced into the reduction layer through the upper lid and the dry layer from above the reduction layer.
  8. 　燃焼室と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置と、前記燃焼室において発生した木炭の燃焼熱により水を過熱して、高温・高圧の過熱水蒸気を発生するようにした過熱水蒸気発生器と、前記木炭水性ガス製造装置において発生した木炭水性ガスを燃料ガスとして供給して発電する燃料電池装置とを備える木炭水性ガス式燃料電池発電システムであって、
    　前記過熱水蒸気発生器において発生した過熱水蒸気を前記木炭水性ガス発生装置が有する還元層へ導入して水性ガス反応を行わせるようにすることを特徴とする燃料電池発電システム。     A charcoal water gas production apparatus comprising: a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer, and a dry layer; and each supply means for supplying charcoal, water, and air to the charcoal water gas generator. A superheated steam generator that superheats water by combustion heat of charcoal generated in the combustion chamber to generate high-temperature and high-pressure superheated steam; and charcoal water gas generated in the charcoal water gas production apparatus as fuel A charcoal water gas fuel cell power generation system comprising a fuel cell device that generates electricity by supplying as gas,
    A fuel cell power generation system characterized in that superheated steam generated in the superheated steam generator is introduced into a reduction layer of the charcoal water gas generator to cause a water gas reaction.
  9. 　前記木炭水性ガス発生装置と過熱水蒸気発生器とを組合せ、かつ、前記過熱水蒸気発生器において発生した過熱水蒸気を前記木炭水性ガス発生装置が有する還元層へ導入して水性ガス反応を行わせるようにする装置は一体化して構成した木炭水性ガス製造装置とし、この一体化して構成した装置は、請求項３ないし７のいずれか１項に記載の装置とすることを特徴とする請求項８に記載の燃料電池発電システム。 The charcoal water gas generator and the superheated steam generator are combined, and the superheated steam generated in the superheated steam generator is introduced into the reduction layer of the charcoal water gas generator so as to cause a water gas reaction. 9. The apparatus according to claim 8, wherein the apparatus configured to be an integrated charcoal water gas production apparatus is the apparatus according to any one of claims 3 to 7. Fuel cell power generation system.
  10. 　前記木炭水性ガス発生装置と前記燃料電池装置との間に、前記木炭水性ガスに含有するＣＯを改質するＣＯ改質機を設け、このＣＯ改質機に、前記過熱水蒸気発生器において発生した過熱水蒸気を供給して、ＣＯをＣＯ2にシフトするシフト反応を行わせるようにすることを特徴とする請求項８または９に記載の燃料電池発電システム。 A CO reformer for reforming CO contained in the charcoal water gas is provided between the charcoal water gas generator and the fuel cell device, and the CO reformer is generated in the superheated steam generator. by supplying superheated steam, fuel cell power generation system according to claim 8 or 9, characterized in that to carry out the shift reaction to shift the CO in the CO 2.
  11. 　前記木炭水性ガス発生装置と前記燃料電池装置との間に、前記燃料電池装置の運転温度に応じて前記木炭水性ガスを冷却または加熱するガス冷却器またはガス加熱装置を設けることを特徴とする請求項８または９に記載の燃料電池発電システム。 A gas cooler or a gas heating device for cooling or heating the charcoal water gas according to an operating temperature of the fuel cell device is provided between the charcoal water gas generator and the fuel cell device. Item 10. The fuel cell power generation system according to Item 8 or 9.
  12. 　前記木炭水性ガス発生装置と前記燃料電池装置との間に、ガス内のダストを除去する徐塵機またはガスフィルタを設けることを特徴とする請求項８ないし１１のいずれか１項に記載の燃料電池発電システム。 The fuel according to any one of claims 8 to 11, wherein a gradual duster or a gas filter for removing dust in the gas is provided between the charcoal water gas generator and the fuel cell device. Battery power generation system.
  13. 　前記燃料電池装置において消費されなかった木炭水性ガスの残ガス（オフガス）のエネルギーを活用するための燃料電池オフガス利用装置を備えることを特徴とする請求項８ないし１２のいずれか１項に記載の燃料電池発電システム。 The fuel cell off-gas utilization device for utilizing the energy of the residual gas (off gas) of the charcoal water gas that has not been consumed in the fuel cell device is provided. Fuel cell power generation system.
  14. 　燃焼室と還元層と乾燥層とを有する縦型円筒状の木炭水性ガス発生装置と、木炭、水および空気を前記木炭水性ガス発生装置へ供給する各供給手段とを備える木炭水性ガス製造装置において、
    　前記還元層と燃焼室とを、燃焼室を外側とし伝熱壁を介して同心円筒状に配設し、前記燃焼室内に熱交換器を設け、この熱交換器に原水タンクから水を供給して水蒸気を発生しこの水蒸気を誘導加熱装置を介して加熱することにより、高温・高圧の過熱水蒸気を発生するようにし、かつ、前記過熱水蒸気と、前記燃焼室において木炭の燃焼により発生したＣＯ2ガスとを、前記還元層に導入するようにしてなり、
    　さらに、前記燃焼室は前記伝熱壁と下部円筒形部とにより形成し、前記還元層は前記伝熱壁と上部円筒形部とにより形成し、前記乾燥層は上部円筒形部により形成し、前記上部円筒形部には木炭水性ガス取出し口と木炭水性ガス発生装置の起動時燃焼空気吸引口とを設け、前記下部円筒形部には木炭投入口兼燃焼空気導入口を設け、かつ前記上部円筒形部の上蓋部には、木炭投入口を設けることを特徴とする木炭水性ガス製造装置。     In a charcoal water gas production apparatus comprising: a vertical cylindrical charcoal water gas generator having a combustion chamber, a reducing layer, and a dry layer; and each supply means for supplying charcoal, water, and air to the charcoal water gas generator ,
    The reduction layer and the combustion chamber are arranged concentrically with the combustion chamber outside and a heat transfer wall, a heat exchanger is provided in the combustion chamber, and water is supplied from the raw water tank to the heat exchanger. Steam is generated and heated through an induction heating device to generate high-temperature and high-pressure superheated steam, and CO 2 generated by combustion of charcoal in the combustion chamber and the superheated steam. Gas is introduced into the reducing layer,
    Further, the combustion chamber is formed by the heat transfer wall and the lower cylindrical portion, the reduction layer is formed by the heat transfer wall and the upper cylindrical portion, and the dry layer is formed by the upper cylindrical portion, The upper cylindrical part is provided with a charcoal water gas outlet and a combustion air suction port at the start of the charcoal water gas generator, the lower cylindrical part is provided with a charcoal inlet and a combustion air inlet, and the upper part An apparatus for producing a charcoal water gas, characterized in that a charcoal inlet is provided in the upper lid of the cylindrical part.
  15. 　前記過熱水蒸気の前記還元層への導入部は、還元層下部、還元層中間部、還元層上部の少なくとも一か所とすることを特徴とする請求項１４に記載の木炭水性ガス製造装置。 15. The apparatus for producing a charcoal water gas according to claim 14, wherein the introduction portion of the superheated steam into the reduction layer is at least one of a lower part of the reduction layer, an intermediate part of the reduction layer, and an upper part of the reduction layer.
  16. 　前記過熱水蒸気の前記還元層への導入部は、リング状に配設した複数個の噴射ノズルを備え、前記噴射ノズルから前記還元層へ過熱水蒸気を噴射して導入することを特徴とする請求項１４または１５に記載の木炭水性ガス製造装置。 The introduction portion of the superheated steam into the reduction layer includes a plurality of injection nozzles arranged in a ring shape, and the superheated steam is injected and introduced from the injection nozzles into the reduction layer. The charcoal water gas production apparatus according to 14 or 15.
PCT/JP2014/069428 2013-07-24 2014-07-23 Charcoal syngas manufacturing method and apparatus, and fuel cell power generation system using said manufacturing method and apparatus WO2015012302A1 (en)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5869291A (en) * 1981-07-08 1983-04-25 Okutama Kogyo Kk Gasification of solid fuel and gas producer
JP2001192675A (en) * 2000-01-12 2001-07-17 Ishikawajima Harima Heavy Ind Co Ltd Method for producing reformed gas from char
JP2004189932A (en) * 2002-12-12 2004-07-08 Kozo Shionoya Apparatus for gasifying solid fuel
JP2006143983A (en) * 2004-10-20 2006-06-08 Mitsui Eng & Shipbuild Co Ltd Method of operating gasifier and gasifier

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5869291A (en) * 1981-07-08 1983-04-25 Okutama Kogyo Kk Gasification of solid fuel and gas producer
JP2001192675A (en) * 2000-01-12 2001-07-17 Ishikawajima Harima Heavy Ind Co Ltd Method for producing reformed gas from char
JP2004189932A (en) * 2002-12-12 2004-07-08 Kozo Shionoya Apparatus for gasifying solid fuel
JP2006143983A (en) * 2004-10-20 2006-06-08 Mitsui Eng & Shipbuild Co Ltd Method of operating gasifier and gasifier

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