WO2013035312A1 - コージェネレーションシステム - Google Patents
コージェネレーションシステム Download PDFInfo
- Publication number
- WO2013035312A1 WO2013035312A1 PCT/JP2012/005606 JP2012005606W WO2013035312A1 WO 2013035312 A1 WO2013035312 A1 WO 2013035312A1 JP 2012005606 W JP2012005606 W JP 2012005606W WO 2013035312 A1 WO2013035312 A1 WO 2013035312A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- heat
- exhaust gas
- cogeneration system
- gas
- heat exchanger
- Prior art date
Links
Images
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
-
- 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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
-
- 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
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M2008/1293—Fuel cells with solid oxide electrolytes
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
- H01M2250/10—Fuel cells in stationary systems, e.g. emergency power source in plant
-
- 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
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B90/00—Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02B90/10—Applications of fuel cells in buildings
-
- 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
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/40—Fuel cell technologies in production processes
Definitions
- the present invention relates to a cogeneration system using a solid oxide fuel cell as a base power source.
- a fuel cell system that includes an SOFC unit and an absorption chiller, and operates the absorption chiller by heating the regenerator of the absorption chiller with combustion exhaust gas discharged from the SOFC unit (patent).
- pattern 2 combustion exhaust gas discharged from the SOFC unit
- the fuel cell system disclosed in Patent Document 1 is a PEFC (polymer electrolyte fuel cell), which has a low operating temperature (60 to 80 degrees) and exhaust gas (combustion exhaust gas) to be discharged. Therefore, the absorption refrigerator refrigeration cycle cannot be driven. That is, it is impossible to realize cogeneration with increased energy efficiency so that the absorption refrigerator is operated using exhaust gas.
- PEFC polymer electrolyte fuel cell
- the fuel cell system disclosed in Patent Document 2 is configured such that moisture mixed as vapor in the exhaust gas can be recovered by exchanging heat between the exhaust gas and water using a heat exchanger.
- the combustion exhaust gas after heating the regenerator of the absorption chiller with the heat of the exhaust gas and driving the absorption chiller still retains high temperature heat.
- the temperature of the exhaust gas is about 100 ° C. at maximum (paragraph of Patent Document 2). [0054]).
- the heat exchanger provided in the fuel cell system of Patent Document 2 is configured to exchange heat between water supplied from tap water or the like and exhaust gas.
- the heat exchanger disclosed in Patent Document 2 cannot be used.
- the fuel cell system disclosed in Patent Document 2 is not configured to be able to make the water balance self-supporting in the system, and the fuel cell system is provided in an area where a water source cannot be obtained. Is not available.
- the present invention has been made in view of the above problems, and an object of the present invention is to provide a cogeneration system that can make the water balance self-supporting in the system.
- a cogeneration system includes a high-temperature operating fuel cell that generates power by a power generation reaction using supplied fuel and air, and the high-temperature operating fuel cell.
- a reformer that generates a reformed gas as the fuel from the supplied raw material gas and water vapor by a reforming reaction using the generated power generation reaction heat and the combustion heat of unused fuel, the power generation reaction heat and the A vaporizer for generating the water vapor to be added to the raw material gas supplied to the reformer using combustion heat, the power generation reaction heat remaining by being used by the reformer and the vaporizer, and A part of the heat of the exhaust gas holding the combustion heat is consumed to cool the object to be cooled, and a part of the heat is used to cool the exhaust gas, and the cooling device holds The exhaust gas after the portion of the heat is consumed by further cooling that, and a condensing unit for generating condensed water by condensing the moisture contained in the exhaust gas.
- the cogeneration system according to the present invention has an effect that the balance of water can be made independent in the system.
- the cogeneration system of the present invention is configured as described above, and has an effect that the balance of water can be made independent in the system.
- FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system in the base station which concerns on Embodiment 1.
- FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system in the base station which concerns on Embodiment 1.
- FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system in the base station which concerns on Embodiment 1.
- FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system in the base station which concerns on Embodiment 1.
- FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system which concerns on the modification 1 of Embodiment 1.
- FIG. It is a schematic diagram which shows an example of a structure of the cogeneration system which concerns on the modification 2 of Embodiment 1.
- FIG. It is a schematic diagram which shows an example of schematic structure of the total heat exchanger in the cogeneration system shown in FIG. It is a schematic diagram which shows an example of schematic structure of the cogeneration system which concerns on the modification 4 of Embodiment 1.
- FIG. It is a figure which shows an example of the material balance in reforming efficiency and a fuel / oxygen utilization rate in the cell reaction which produces
- FIG. 13 is a schematic diagram illustrating an example of a schematic configuration of a current base station.
- the base station shelter 200 includes a BTS (Base Transceiver System) 211 and an air conditioner (AC) 212, and a power management system (PMS) 213 including a backup storage battery (SB) 219. It has.
- BTS Base Transceiver System
- AC air conditioner
- PMS power management system
- SB backup storage battery
- the PMS 213 converts the power (for example, AC 220V) from the DG 202 and GRID 201 to the power for driving the BTS 211 (for example, DC 48V) and supplies it. Further, the PMS 213 also performs power management corresponding to the continuous power consumption of the BTS 211 such as performing backup by the SB 219 until the power from the GRID 201 is interrupted and the DG 202 is activated.
- the AC 212 adjusts the room temperature so that the temperature in the base station shelter 200 does not exceed the temperature at which the BTS 211 can operate. Specifically, the room temperature is adjusted so that the temperature in the base station shelter 200 is about 35 ° C.
- PUE Power Usage Efficiency
- a base station is a facility that is inferior in energy efficiency even when compared with other facilities by applying an index called PUE (Power Usage Efficiency).
- the base station is applied to this index, the PUE reaches 5 or more, and the energy efficiency is poor.
- a factor that reduces the energy efficiency of such base stations is that a cooling facility such as AC212 is required.
- the operating ambient temperature of the BTS 211 in the base station shelter 200 is about 35 ° C. or less as described above. This is because if a power element (power MOS-FET or the like: a member that requires cooling) mounted on the power amplifier unit included in the BTS 211 exceeds the temperature, there is a risk of thermal damage. For this reason, the temperature in the base station shelter 200 needs to be constantly controlled by the AC 212 so as to be 35 degrees or less.
- the power consumption of the BTS 211 itself is 1 KW or less at the maximum, but the power consumption of the AC 212 that performs cooling necessary to drive the BTS 211 is about 4 KW at the maximum. That is, in the base station, the amount of power consumed by the AC 212 that manages the room temperature so that the BTS 211 can operate is larger than the amount of power consumed by the operation of the BTS 211. For this reason, the power consumption of the base station depends on the outside air temperature that directly affects the room temperature in the base station shelter 200 rather than the required power of the BTS 211.
- an absorption refrigerator that is driven using exhaust heat generated by power generation.
- the cogeneration that was used is effective.
- diesel engines (DE), gasoline engines (GE), micro gas turbines (MGT), etc. that are commonly used as distributed power engines like current base stations are all effective in supplying power to small-scale power consumption equipment.
- the exhaust heat temperature of MGT is about 250 ° C.
- exhaust heat having a sufficient amount of heat to drive the absorption refrigerator can be obtained.
- the MGT generates power of about 100 KW or more, such as factory equipment, and it is difficult to reduce the size so that the base station generates power of about several KW or less.
- the power consumption at the base station depends on the outside air temperature surrounding the base station shelter 200 as described above. For this reason, the required amount of cooling energy varies depending on the season or time of day. That is, the demand ratio of electricity and heat (electric heat ratio) varies depending on time and season, and it is difficult to apply the conventional cogeneration assuming a constant electric heat ratio.
- a fuel cell having the following advantages is adopted as a backup power source for the base station.
- the fuel cell does not depend on the size of the power consumption equipment, and the power generation efficiency can be flexibly dealt with greatly changing power consumption.
- the fuel cell does not stop power generation due to changes in the natural environment or the like, and can continuously obtain desired power.
- SOFC solid oxide fuel cells
- MCFC molten carbonate fuel cells
- the present invention provides the following aspects.
- the cogeneration system includes a high-temperature operation type fuel cell that generates power by a power generation reaction using supplied fuel and air, and power generation reaction heat generated in the high-temperature operation type fuel cell.
- a reformer that generates a reformed gas to be the fuel from the supplied raw material gas and water vapor by a reforming reaction using the combustion heat of unused fuel, and the power generation reaction heat and the combustion heat
- a vaporizer for generating the steam to be added to the raw material gas supplied to the reformer, and the power generation reaction heat and the combustion heat remaining used by the reformer and the vaporizer.
- the high-temperature operation type fuel cell means a fuel cell having an operation temperature of 400 ° C. or higher.
- Examples of the high temperature operation type fuel cell include a solid oxide fuel cell (SOFC) cell or a molten carbonate fuel cell (MCFC) cell.
- SOFC solid oxide fuel cell
- MCFC molten carbonate fuel cell
- the carburetor, the reformer, and the high-temperature operation type fuel battery cell are provided, power is generated from the supplied air and the reformed gas (fuel) generated from the raw material gas.
- the cooling device since the cooling device is provided, it is possible to suitably cool an object to be cooled such as a member, a substance, or a space that needs to be cooled. That is, it is possible to perform cogeneration that increases the energy efficiency by consuming part of the heat held by the exhaust gas generated during power generation of the high-temperature operating fuel cell and operating the cooling device. Furthermore, when the cooling device is operated, the exhaust gas can be cooled by consuming part of the heat held by the exhaust gas.
- the cooling device consumes part of the heat it holds, further cools the exhaust gas after cooling, and condenses moisture contained in the exhaust gas to produce condensed water can do.
- the water generated in the system can be recovered to cover the water required for power generation of the high-temperature operating fuel cell.
- the cogeneration system according to the first aspect of the present invention has an effect that the balance of water can be made independent in the system.
- the cogeneration system which concerns on the 2nd aspect of this invention is the above-mentioned 1st aspect.
- WHEREIN The said condensation unit utilizes the heat
- the solid oxide fuel cell using the first heat exchanger that heats the raw material gas supplied to the vaporizer and the heat of the exhaust gas that has been used by the first heat exchanger.
- a second heat exchanger that heats supplied air and condenses water contained in the exhaust gas to generate condensed water may be provided.
- the condensing unit since the condensing unit includes the first heat exchanger and the second heat exchanger, all the heating to the source gas and the heating to the air can be performed using the heat held by the exhaust gas. it can.
- heated air can be supplied to the high temperature operation type fuel cell, and heated raw material gas can be supplied to the vaporizer. Therefore, it is possible to suppress the heat energy necessary for increasing the temperature of the air and the heat energy necessary for adding water to the raw material gas, and as a result, the temperature of the heat held by the exhaust gas can be increased. . Thereby, the energy (exergy) which can be taken out from exhaust gas can be raised.
- the cooling by the cooling device, the heating to the raw material gas by the first heat exchanger, and the heating to the air by the second heat exchanger are performed using the heat held by the exhaust gas. For this reason, the heat possessed by the exhaust gas is consumed, and finally the temperature of the exhaust gas is reduced to such an extent that the amount of water required for power generation of the high temperature operation type fuel cell can be obtained (for example, about 40 ° C.). Can be made. For this reason, in the cogeneration system according to the second aspect of the present invention, water generated in the system can be recovered to supply water necessary for power generation of the high-temperature operating fuel cell.
- the cogeneration system according to a third aspect of the present invention is the cogeneration system according to the second aspect described above, wherein the first heat exchanger uses the heat of the exhaust gas after a part of the heat is consumed by the cooling device.
- the total heat exchanger may be used that heats the raw material gas supplied to the vaporizer and humidifies it with moisture contained in the exhaust gas.
- the raw material gas can be heated and humidified using the heat of the exhaust gas.
- the heated and humidified raw material gas can be supplied to the vaporizer. Therefore, it is possible to suppress the thermal energy required when water is added to the raw material gas, and as a result, it is possible to increase the temperature of the heat retained by the exhaust gas. Thereby, the energy (exergy) which can be taken out from exhaust gas can be raised.
- the condensing unit cools the exhaust gas after heat is consumed by the cooling device by air cooling.
- the exhaust gas is cooled by the blower, and the water contained in the exhaust gas is condensed to generate condensed water.
- the temperature of the exhaust gas can be lowered to an extent (for example, about 40 ° C.) where a necessary amount of water can be obtained at the time of power generation of the high temperature operation type fuel cell.
- moisture generated in the system can be recovered and supplied as water necessary for power generation of the high temperature operation type fuel cell.
- the cogeneration system according to a fifth aspect of the present invention is the cogeneration system according to any one of the first to fourth aspects described above, wherein the vaporizer uses the power generation reaction heat and the combustion heat to generate the condensed water.
- the water vapor may be generated by evaporating the water vapor.
- the cooling device is an absorption-type cooling device that causes the refrigerant to absorb and circulate the refrigerant.
- the boiling point temperature of the refrigerant is lower than that of the absorbing liquid, and heat is generated between the exhaust gas and the absorbing liquid that has absorbed the refrigerant in order to separate the refrigerant from the absorbing liquid that has absorbed the refrigerant.
- a third heat exchanger to be replaced may be provided, and the absorbing liquid that has absorbed the refrigerant may be vaporized by heat obtained by heat exchange by the third heat exchanger.
- the cogeneration system according to a seventh aspect of the present invention is the cogeneration system according to the sixth aspect, wherein the absorption cooling device liquefies only the absorption liquid from the vaporized absorption liquid that has absorbed the refrigerant.
- a fourth heat exchanger that exchanges heat with air, and supplies the air heated by the heat exchange with the vaporized refrigerant by the fourth heat exchanger to the high-temperature operating fuel cell. It may be configured.
- the absorption cooling device since the absorption cooling device includes the fourth heat exchanger, the refrigerant vaporized in the absorption cooling device can be cooled and liquefied, and the high-temperature operation fuel cell The air supplied to the cell can be further preheated.
- the condensed water condensed from the exhaust gas by the second heat exchanger is transported to the first heat exchanger.
- a water transport part is provided, and the condensed water transported by the water transport part and the exhaust gas are mixed to produce exhaust gas containing the condensed water as steam, and the steam contained in the exhaust gas by the first heat exchanger May be configured to heat and humidify the source gas.
- the condensed water condensed from the exhaust gas can be transported to the first heat exchanger.
- the condensed water transported to the first heat exchanger is vaporized by the high-temperature exhaust gas and circulates through the first heat exchanger while being contained in the exhaust gas. That is, the exhaust gas in a state containing a large amount of water vapor heats the raw material gas and humidifies it in the first heat exchanger. For this reason, in the said 1st heat exchanger, the raw material gas supplied to a high temperature operation type fuel cell can be humidified efficiently.
- the cogeneration system is the mixing system according to the eighth aspect described above, wherein a part of the reformed gas generated in the reformer is diverted and mixed with the raw material gas.
- a reduction reaction unit that generates hydrogen sulfide by reducing a sulfur compound contained in a raw material gas from a gas, and an adsorption unit that adsorbs and removes hydrogen sulfide generated by the reduction reaction unit.
- exhaust gas to be supplied to the cooling device may be supplied, and the reaction temperature in the reduction reaction unit may be maintained by heat transmitted from the exhaust gas.
- a cogeneration system includes, in any one of the first to ninth aspects described above, a power storage device that stores power generated by the high temperature operation type fuel cell. May be.
- the cogeneration system according to an eleventh aspect of the present invention is the cogeneration system according to any one of the first to tenth aspects described above, wherein the cooling device is operated by electric power generated by the high temperature operation type fuel cell.
- the facility equipment to be configured may be configured to cool at least a cooling-necessary member that needs to be cooled as the object to be cooled.
- the equipment is operated by the electric power generated by the high temperature operation type fuel cell
- the cooling device is operated by the exhaust gas generated during the power generation of the high temperature operation type fuel cell, thereby cooling the cooling necessary members of the equipment device. can do. That is, it is possible to perform cogeneration that increases the energy efficiency by operating the cooling device with the exhaust gas generated during power generation of the high-temperature operation type fuel cell.
- an upper limit value of the temperature at which the cooling-required member is to be cooled is determined, and the cooling device is a cooling-required member. May be configured to cool so that the temperature becomes lower than the predetermined upper limit value.
- the power generation amount of the high temperature operation type fuel cell is controlled based on the temperature information of the cooling required member. You may be comprised so that.
- the power generation amount of the high-temperature operation type fuel cell is controlled based on the temperature information of the member requiring cooling.
- the operation of the high-temperature operating fuel cell and the amount of power generation can be controlled in accordance with the demand for heat, such as keeping the temperature of the member requiring cooling at a temperature below a certain level.
- the reliability of the system can be improved.
- the cogeneration system according to a fourteenth aspect of the present invention is the cogeneration system according to any one of the first to tenth aspects, wherein the cooling device is cooled by the condensing unit as the cooling object.
- the exhaust gas may be further cooled to further condense the moisture contained in the gas to produce condensed water.
- the exhaust gas cooled by the condensing unit can be further cooled by the cooling device. And the moisture contained in exhaust gas can be further condensed, and condensed water can be produced
- FIG. 1 is a schematic diagram illustrating an example of a schematic configuration of a cogeneration system 100 in a base station according to the first embodiment.
- the cogeneration system 100 mainly includes an SOFC system (high temperature operation type fuel ionization system) 101 functioning as a power generation device, and a BTS (equipment equipment) in a base station shelter that uses power generated by the SOFC system 101. ) 11 and an ammonia absorption refrigerator (cooling device, absorption cooling device) 10 for cooling the power element of the power amplifier section included in the BTS 11.
- SOFC system high temperature operation type fuel ionization system
- BTS equipment
- ammonia absorption refrigerator cooling device, absorption cooling device
- the cogeneration system 100 further includes a power management system (PMS) 12 including a backup storage battery (SB (power storage device) 19) and a diesel engine (DG) (not shown) as an auxiliary power source.
- PMS power management system
- the BTS 11 is supplied with power from the SOFC system 101, and is configured to be able to receive power from the SB 19 or DG via the PMS 12 when the supply of power is interrupted or shortage. ing.
- the base station is provided in an area where GRID is not developed, and is configured to supply power from the SOFC system 101 to the BTS 11 instead of supplying power from the GRID to the BTS 11. Furthermore, the base station is provided in an area where a water source such as industrial water cannot be obtained.
- the SOFC system 101 collects water contained in the exhaust gas and supplies it to the vaporizer 15 of the SOFC hot module 1 described later. It is configured to operate.
- the regenerative heat exchanger (third heat exchanger) 51 is heated by the heat of the exhaust gas discharged from the SOFC hot module 1 of the SOFC system 101, and the ammonia absorption refrigerator 10 is heated.
- the aqueous ammonia solution is vaporized using the regenerative heat exchanger 51 as a heat source.
- the cogeneration system 100 includes the ammonia absorption refrigerator 10 as a heat load, the BTS 11 as a power load, and the SOFC system 101 as a power generator. Note that power generation control in the SOFC cell (high temperature operation fuel cell) 13 in the SOFC system 101 is performed according to power consumption related to communication in the base station.
- the SOFC system 101 is a power generation system that uses a SOFC (solid oxide fuel cell) as a fuel cell.
- the SOFC system 101 includes a SOFC hot module 1, a drain tank 2, a fuel processor (FPS) 3, a condensing unit 30, a blower 9, and a first condensed water pump 20.
- SOFC solid oxide fuel cell
- the SOFC hot module 1 functions as a power generator in the cogeneration system 100, and includes an SOFC cell 13 having an anode 22 and a cathode 23 therein, a combustion unit 14, a vaporizer 15, and a reformer 16.
- the SOFC cell 13 is a power generation unit, and a current collecting member 17 is provided. Although omitted in FIG. 1, the SOFC cell 13 is electrically connected to the BTS 11 that is a power load via the current collecting member 17 via a power converter (not shown).
- the reformer 16 is for steam reforming a fuel (raw material) gas such as city gas. Water used for the steam reforming is vaporized by the vaporizer 15 and added to the fuel gas. It is configured to be supplied to the mass device 16.
- a combustion unit 14 is provided between the SOFC cell 13 and the reformer 16 and the vaporizer 15, and the reforming reaction heat (reforming reaction energy) required for the reformer 16 and the vaporization are provided.
- the heat of vaporization (water evaporation energy) required in the vessel 15 is covered by the heat generated in the combustion section 14.
- the SOFC system 101 is configured to perform heat exchange between the exhaust gas discharged from the SOFC hot module 1 and the refrigerant (ammonia) by the regenerative heat exchanger 51 of the ammonia absorption refrigerator 10. That is, the ammonia absorption refrigerator 10 consumes a part of the heat of the exhaust gas to cool the object to be cooled (the power element of the power amplifier unit included in the BTS 11) and consumes a part of the heat.
- the exhaust gas discharged from the SOFC hot module 1 is cooled.
- the SOFC system 101 is configured to further cool the exhaust gas after heat is consumed by the heat exchange described above, and to condense moisture from the exhaust gas. More specifically, in the SOFC system 101 according to the first embodiment, the exhaust gas after the heat is consumed by the heat exchange described above is further dissipated in the condensing unit 30 to the extent that moisture can be condensed from the exhaust gas. The temperature of the exhaust gas is lowered. For this reason, the SOFC system 101 can recover water from the exhaust gas.
- condensation unit 30 included in the SOFC system 101 according to the first embodiment will be described more specifically.
- FIG. 2 is a schematic diagram illustrating an example of a schematic configuration of the cogeneration system 100 in the base station according to the first embodiment.
- the condensing unit 30 circulates the exhaust gas and the blower fan (blower) 31 driven by a motor in order to dissipate heat so as to reduce the temperature of the exhaust gas to the extent that moisture can be condensed from the exhaust gas.
- a radiator 32 a radiator.
- circulates the radiator 32 is cooled with the ventilation fan 31 by air cooling.
- the condensing unit 30 By setting the condensing unit 30 to such a configuration, the temperature of the exhaust gas can be lowered to the extent that moisture can be condensed from the exhaust gas. For this reason, water can be recovered from the exhaust gas.
- the condensing unit 30 not only cools the exhaust gas by the blower fan 31 described above, but also exchanges heat between the supplied fuel (raw material) gas and the exhaust gas using a heat exchanger, and further efficiently reduces the temperature of the exhaust gas. It is good also as a structure.
- the condensing unit 30 is configured to further include a total heat exchanger 7 as a heat exchanger for performing heat exchange between the fuel (raw material) gas and the exhaust gas.
- FIG. 3 is a schematic diagram illustrating an example of a schematic configuration of the cogeneration system 100 in the base station according to the first embodiment.
- the exhaust gas that has undergone heat exchange in the regenerative heat exchanger 51 of the ammonia absorption refrigerator 10 flows into the total heat exchanger 7, while the fuel (raw material) gas supplied to the SOFC hot module 1 also has this total heat. It is configured to flow into the exchanger 7.
- total heat exchanger 7 total heat exchange is performed between the exhaust gas and the fuel (raw material) gas by the total heat exchanger 7.
- the exhaust gas after the total heat exchange can be cooled by the blower fan 31, and water can be recovered from the exhaust gas.
- heat exchange means exchanging only heat without mass transfer
- total heat exchange means exchanging heat with mass transfer
- the condensation unit 30 can efficiently reduce the temperature of the exhaust gas by the total heat exchange between the exhaust gas and the fuel (raw material) gas in the total heat exchanger 7 and the cooling of the exhaust gas by the blower fan 31. it can.
- the fuel (raw material) gas is heated and humidified by transferring heat contained in the exhaust gas and moisture contained in the exhaust gas.
- the temperature of the exhaust gas discharged from the SOFC hot module 1 can be increased.
- the fuel (raw material) gas can be humidified, the amount of reforming water supplied to the reformer 16 can be reduced.
- FIG. 4 is a schematic diagram illustrating an example of a schematic configuration of the cogeneration system 100 in the base station according to the first embodiment.
- the condensing unit 30 performs total heat exchange between the fuel (raw material) gas and the exhaust gas by the total heat exchanger 7. And it is set as the structure which further heat-exchanges by the condensation heat exchanger 8 between the waste gas after total heat exchange, and the air supplied to the SOFC hot module 1.
- the cogeneration system 100 can reduce the temperature of the exhaust gas to such an extent that moisture can be condensed from the exhaust gas. For this reason, water can be recovered from the exhaust gas. Furthermore, since fuel (raw material) gas and air can be preheated and supplied to the SOFC hot module 1, the temperature of the exhaust gas discharged from the SOFC hot module 1 can be increased.
- the total heat exchanger 7 includes a fuel passage portion 72 that allows the passage of fuel (raw material) gas and a heating portion 71 that allows the passage of exhaust gas, as shown in FIG. Further, the heating part 71 and the fuel passage part 72 are separated by a selectively permeable membrane 73 that selectively permeates moisture. In this total heat exchanger 7, the water vapor contained in the exhaust gas passing through the heating part 71 is totally exchanged with the fuel gas passing through the fuel passage part 72 through the permselective membrane 73 (heat exchange accompanied by movement of substances). ) This heats and humidifies the fuel (raw material) gas.
- the condensing unit 30 includes the total heat exchanger 7 and performs a total heat exchange between the exhaust gas and the fuel (raw material) gas.
- the heat of the exhaust gas may be transferred to the fuel (raw material) gas.
- the heat exchanger which performs heat exchange between exhaust gas and fuel (raw material) gas instead of the total heat exchanger 7 may be used.
- the fuel (raw material) gas can be heated and humidified, the total heat exchanger 7 is preferable.
- the SOFC hot module 1 is supplied with fuel (raw material) gas and air. Before the fuel (raw material) gas is supplied to the SOFC hot module 1, impurities are removed by a fuel processor (FPS) 3. The fuel (raw material) gas is heated and humidified by the total heat exchange with the exhaust gas discharged from the SOFC hot module 1 by the total heat exchanger 7 and supplied to the SOFC hot module 1.
- FPS fuel processor
- the fuel (raw material) gas supplied to the SOFC hot module 1 is sent to the vaporizer 15.
- vaporized water is added to the fuel (raw material) gas and supplied to the reformer 16 as a mixed gas with water vapor.
- the exhaust air exhausted from the cathode 23 and the exhaust hydrogen exhausted from the anode 22 are combusted in the combustion unit 14.
- the combustion energy is used as heat of vaporization of water consumed by the vaporizer 15 (water evaporation energy) and reforming reaction heat consumed by the reformer 16 (reforming reaction energy).
- the SOFC system 101 is started, the unreformed raw material is combusted in the combustion section 14 and the SOFC hot module 1 is preheated.
- the temperature of heat required for the reforming reaction in the reformer 16 is about 650 ° C., and the amount of added water required for the reforming reaction is S / C (steam carbon ratio; water and carbon in the raw fuel).
- the molar ratio) is at least 2.0 or more, generally about 2.5 to 3.0.
- the SOFC hot module 1 is controlled so that these conditions are maintained, and generates a hydrogen-rich reformed gas from the raw material and the reformed water.
- the reformed gas generated by the reformer 16 is supplied to the anode 22 of the SOFC cell 13, and air is supplied from the blower 9 to the cathode 23, and the reaction shown in the following formula (1) is performed electrochemically. Is called. H 2 + 1 / 2O 2 ⁇ H 2 O (1)
- This reaction is similar to the hydrogen combustion reaction.
- the basic principle of a fuel cell is to electrochemically extract energy corresponding to the combustion energy obtained by this combustion reaction.
- heat power generation waste heat
- the battery operating temperature is about 700 ° C.
- the SOFC hot module 1 included in the SOFC system 101 according to the first embodiment as a result, the power generation waste heat of the SOFC cell 13 and the combustion heat of the surplus reformed gas are converted into the vaporizer 15 and the reformer 16. Used for driving. Further, the SOFC cell 13 is driven by the reformed gas generated by the driven vaporizer 15 and the reformer 16. That is, the SOFC hot module 1 constitutes a kind of power regeneration mechanism.
- the combustion exhaust gas discharged from the SOFC hot module 1 is a gas obtained after the power generation waste heat of the SOFC cell 13 and the combustion heat of the surplus reformed gas are used for driving the vaporizer 15 and the reformer 16.
- the fuel cell generated water and the combustion generated water are contained in the form of water vapor.
- the temperature of this exhaust gas will be about 250 degreeC. For this reason, this exhaust gas can be used for heating the ammonia absorption refrigerator 10.
- the SOFC system 101 includes a fuel processor (FPS) 3 and is configured to remove impurities.
- FPS fuel processor
- SOFC has a higher operating temperature than PEFC.
- SOFC has the advantage that it has higher chemical resistance than PEFC in terms of the adsorption / desorption characteristics of impurities to the catalyst.
- SOFC is anionic (anion is supplied from the cathode and reacts at the anode), it has the advantage that most of the low-molecular volatile impurities burn at the anode.
- the fuel processor (FPS) 3 is equipped with various filters that remove these impurities mainly by washing with water, adsorption, etc., and purifies the raw material (fuel) gas. In particular, desulfurization is performed by a desulfurization filter in the fuel processor 3. When the content of the sulfur compound in the raw material (fuel) gas is small, the fuel processor (FPS) 3 may be omitted.
- the ammonia absorption refrigerator 10 includes a regenerative heat exchanger 51, a rectifier 52, a radiator 54, an absorber 56, and a reservoir 57, and water as an absorbent and ammonia as a refrigerant. Is used. In other words.
- the ammonia absorption refrigerator 10 uses an ammonia and water mixed medium as a working fluid.
- the aqueous ammonia solution stored in the reservoir 57 is heated by the heat source in the regenerative heat exchanger 51 and vaporized.
- This water-ammonia mixture is fractionated by the rectifier 52, and water having a high boiling point is returned to the storage device 57 and the absorber 56 through the regenerative heat exchanger 51, and only ammonia having a low boiling point passes through the rectifier 52. It passes through and is supplied to the radiator 54.
- the radiator 54 acts to cool and liquefy the ammonia vapor.
- Liquid ammonia obtained by releasing heat by being cooled by the radiator 54 is supplied to the cooler 55 through a thin tube.
- the liquid ammonia having a high concentration in the cooler 55 is vaporized and absorbed by the water in the absorber 56.
- cooling is performed by removing the latent heat of evaporation from the object to be cooled (BTS11).
- the ammonia absorption chiller 10 reduces the heat of the exhaust gas supplied to the regenerative heat exchanger 51, and cools the cold output from the ammonia absorption chiller 10 to the cooler 55. Can be taken out from.
- the COP of the ammonia absorption refrigerating machine 10 is 0.5 to 0.6, and a cold heat of 0.5 to 0.6 can be output with respect to the input heat of 1.0. . Further, it is possible to take out a cold output that is roughly proportional to the input heat energy.
- the steam generation temperature in a generator (not shown) provided in the ammonia absorption refrigerator 10 is about 100 to 160 ° C.
- the exhaust gas discharged from the SOFC hot module 1 is about 250 ° C., the ammonia absorption refrigerator 10 can be driven.
- the higher the steam generation temperature the lower the cooling temperature. Therefore, if the flow rate of exhaust gas discharged from the SOFC hot module 1 is the same, the higher the temperature of the exhaust gas, the greater the cold output. Moreover, since the cold heat output by the ammonia absorption refrigerator 10 increases as the temperature of the exhaust gas increases, the heat exchange area of the regenerative heat exchanger 51 can be reduced to reduce the size of the apparatus.
- the power consumption in the BTS 11 is about 800 W at the maximum load, and the breakdown is 300 W in the control amplifier unit (not shown) that controls the signal processing, and the power amplifier unit that amplifies this signal and converts it into radio waves
- the power consumption is 300 W (not shown)
- the power consumption of auxiliary power such as an air cooling fan (not shown) is 200 W.
- the amplifier efficiency of the power amplifier section has been improving year by year, and about 40% is the mainstream nowadays.
- the power amplification efficiency of 40% means that 100 W of power is required to output a 40 W power amplification signal, and the remaining 60 W corresponds to heat generation. That is, the heat generation in the power element of the power amplifier unit increases as the energy consumption (communication energy) related to communication increases. In other words, the power element ambient temperature T depends on the magnitude of communication energy.
- the heat-resistant temperature of general electronic parts is about 70-80 ° C
- the control amplifier unit that handles weak electric power basically does not need to be cooled, or regardless of the outside air temperature (for example, at an outside air temperature of 50 degrees). Cooling with normal fan air cooling is sufficient.
- power elements used in the power amplifier section will reach 200 ° C. or higher due to the above-mentioned heat generation unless they are cooled, and will be destroyed beyond the junction heat resistance temperature (about 170 ° C. for Si elements). . Further, since the temperature generated by the heat generation is high, sufficient cooling cannot be realized by the above-described fan air cooling by the air cooling fan.
- the BTS 11 can be cooled using the ammonia absorption refrigerator 10 described above so that the temperature (power element ambient temperature T) during operation of the BTS 11 is 35 degrees or less. It has become.
- the cogeneration system 100 in order to stably operate the BTS 11 having a maximum power consumption of 800 W, the amount of heat that needs to be forcibly removed is 60% of 300 W, that is, the amount of heat corresponding to 180 W.
- the configuration in which the entire interior of the base station shelter is cooled to 35 ° C. or lower is inefficient. Therefore, the cogeneration system 100 according to the first embodiment is configured to directly cool a portion (power element of the power amplifier unit) that requires forced cooling instead of cooling the entire base station shelter. . Then, the power generation amount in the SOFC system 101 is controlled so that the power element ambient temperature T is equal to or lower than a predetermined temperature (35 ° C. or lower).
- the base station can operate stably regardless of the outside air temperature by giving a cooling amount proportional to communication energy. it can.
- the generated electric heat ratio and the consumed electric heat ratio are constant regardless of the outside temperature of the base station.
- the value of the electrothermal ratio is a numerical value obtained by dividing the consumed or generated power by the consumed or generated heat. For example, in the case of a device that consumes 1000 W of power and consumes 500 W of cold, the value of the power consumption ratio is 2. In the case of an apparatus that consumes 1000 W of power and consumes 200 W of cold, the value of the power consumption ratio is 5.
- the generated heat amount is the exhaust gas temperature discharged from the SOFC hot module 1, that is, the power generation reaction heat and the combustion heat of unused fuel are used by the vaporizer 15 and the reformer 16.
- the amount of heat consumed is the amount of heat generated by consuming power in the BTS 11 at the power amplifier unit.
- the cogeneration system 100 is configured to control the power generation of the SOFC cell 13 so that the value of the generated heat-to-heat ratio is constant regardless of the outside air temperature.
- the cogeneration system 100 is configured such that the value of the ratio between the electric power generated by the power generation of the SOFC cell 13 and the amount of heat generated in association with this power generation (the value of the generated electric heat ratio) is the power amplifier unit of the BTS 11. It is configured to be the same as or smaller than the value of the ratio of the power consumed in the above and the amount of heat generated in relation to this consumption (value of the power consumption ratio).
- a base station can implement
- the cogeneration system 100 is physically isolated, cannot be expected to have other incidental power sources, and has a severe climate where the outside air temperature varies greatly in time and season. It can be used as a fuel supply system for installed base stations.
- the power consumption consumed by the BTS 11 depends on the amount of communication, and even if the power consumption is 800 W at the maximum, it is about 400 W when converted to the average output during use. For this reason, it is not necessary to design the maximum output of the power generated by the SOFC cell 13 to be 800 W.
- the maximum output of the SOFC cell 13 is designed to be 500 W, which is slightly higher than the average output, and at the time of average output, the surplus power obtained from this is stored in the SB 19. Further, the temperature at which the power amplifier unit is cooled by the ammonia absorption refrigerator 10 is further excessively cooled below 35 ° C.
- the cooling temperature is excessively cooled so as to be 35 ° C. or less in advance, and the heat generated when the BTS 11 is operated at the maximum output is obtained by excessive cooling and cooling of the ammonia absorption refrigerator 10. Can be dealt with by the cold heat.
- the cogeneration system 100 has a substantially constant electric power consumption ratio and generated electric heat ratio. For this reason, instead of performing power generation control of the SOFC cell 13 in accordance with power consumption related to communication in the base station, power generation control may be performed in accordance with power consumption in the power element of the power amplifier unit.
- the cogeneration system 100 heats and operates to generate power according to the heat demand, for example, keeping the refrigerant bath temperature below a certain level (eg, 70 ° C. or below) Necessary power supply can be realized by simple control by the main slave. Thereby, it can operate
- the value of the generated electric heat ratio of the BTS 11 is 800 W (generated power): 180 W (generated heat amount) at the maximum output, that is, about 4.
- the supply and demand of electric power and cold energy can be balanced by obtaining the cold energy corresponding to the heat quantity of 180 W with the value 4 of the generated electric heat ratio.
- the cogeneration system 100 when configured so as to generate 300 W of cold for the electric power of 800 W at the maximum output, the cold of about 100 W becomes a surplus.
- the cogeneration system 100 excessively cools the power element.
- this excessive cooling has no problem in the operation of the power element.
- the value of the generated electric heat ratio is 8, that is, a configuration in which only a heat amount of 100 W is obtained with respect to the generated electric power of 800 W, the power element is destroyed due to insufficient cooling capacity, which becomes a problem.
- the power generation efficiency is the same, it can be said that the larger the amount of heat obtained from the unit power generation at this time, that is, the smaller the value of the generated electric heat ratio, the better.
- the cogeneration system 100 shown in FIG. 4 is configured to increase the exhaust gas temperature of the SOFC hot module 1 and improve the available exergy of the ammonia absorption refrigerator 10 by the following three methods.
- the exhaust gas discharged from the SOFC hot module 1 contains SOFC battery reaction product water and combustion product water.
- the exhaust gas is supplied to the total heat exchanger 7 after a predetermined amount of heat is used in the ammonia absorption refrigerator 10 that is a heat load.
- the generated heat exchanger temperature in the ammonia absorption refrigerator 10 is about 150 ° C., and 150 ° C. exhaust gas is supplied to the total heat exchanger 7.
- the fuel gas sent to the SOFC hot module 1 is also supplied to the total heat exchanger 7 together with the exhaust gas described above. Therefore, the total heat exchanger 7 converts the water vapor contained in the exhaust gas supplied via the ammonia absorption refrigerator 10 into fuel (raw material) gas using the selectively permeable membrane 73 provided in the total heat exchanger 7. Move (total heat exchange). Thereby, the water vapor contained in the exhaust gas and the heat held by the water vapor are transferred to the fuel gas.
- the fact that the steam contained in the exhaust gas and the heat held by the steam are transferred to the fuel (raw material) gas by the total heat exchanger 7 means that the reforming reaction heat consumed by the reformer 16 (reforming vaporization). It is equivalent to recovering a part of the energy) from the exhaust gas. For this reason, the reforming reaction heat (reforming vaporization energy) consumed in the SOFC hot module 1 can be reduced without changing the fuel consumption rate. As a result, the temperature of the exhaust gas discharged from the SOFC hot module 1 can be increased, thereby increasing the amount of energy for driving the ammonia absorption refrigerator 10 provided at the subsequent stage of the SOFC hot module 1. That is, although the power generation efficiency is constant, the value of the generated electric heat ratio can be lowered as a result. Furthermore, transferring the water vapor contained in the exhaust gas to the fuel gas means recovering and reusing the water. For this reason, it leads to the realization of the water balance independence in the base station constructed in the location condition where the water source cannot be obtained.
- the cogeneration system 100 further includes the condensation heat exchanger 8 as described above.
- the exhaust gas that has undergone total heat exchange by the total heat exchanger 7 is supplied to the condensing heat exchanger 8 and air to be sent to the SOFC hot module 1 is supplied.
- the condensation heat exchanger 8 exchanges heat between the air and the exhaust gas, and as a result, the air sent to the SOFC hot module 1 can be preheated.
- the cogeneration system 100 can send the preheated air to the SOFC hot module 1 and reduce the heat of vaporization consumed in the SOFC hot module 1. Can do. Thereby, the temperature of the exhaust gas discharged from the SOFC hot module 1 can be increased.
- the temperature of the exhaust gas can also be lowered until condensed water can be generated by heat exchange with the air by the condensation heat exchanger 8.
- the condensed water obtained from the exhaust gas is stored in the drain tank 2 as reformed water.
- the condensed water stored in the drain tank 2 is supplied to the vaporizer 15 in the SOFC hot module 1 by the first condensed water pump 20.
- the water vapor contained in the exhaust gas can be stored in the drain tank 2 as reformed water, and the stored condensed water can be supplied to the vaporizer 15.
- the water balance can be independent. A specific description of water balance independence will be described later.
- power can be supplied from an auxiliary power source (for example, solar power or wind power generation) other than the SOFC cell 13 to a power converter (not shown). It is configured to be able to.
- an auxiliary power source for example, solar power or wind power generation
- the cogeneration system 100 is configured not to perform power generation control of the SOFC cell 13 in accordance with power consumption related to communication, but to perform cooling control by heat main power.
- the value of the generated electric heat ratio is small, it is not possible to cover all the required power from the SOFC cell 13. In such a case, it is preferable that power is supplied also from the auxiliary power source.
- the renewable energy such as exhaust gas supplied to the ammonia absorption refrigerator 10 does not bother to consume fuel to obtain itself. Therefore, fuel consumption can be reduced by using the SOFC cell 13 as a base load power source and performing power management using an auxiliary power source in combination. By reducing fuel consumption in this way, there are operational advantages such as reducing the frequency of replacement of fuel cylinders, for example.
- modified examples (modified examples 1 to 4) of the cogeneration system 100 according to the first embodiment shown in FIG. 4 will be described.
- FIG. 5 is a diagram illustrating an example of a schematic configuration of the cogeneration system 100 according to the first modification of the first embodiment. Except for the point that the radiator 54 is replaced with the refrigerant condensing heat exchanger 58, the configuration is the same as that of the cogeneration system 100 shown in FIG. .
- the refrigerant vapor can be cooled and condensed in the ammonia absorption refrigerator 10, and the air sent to the SOFC hot module 1 can be further preheated.
- this modification 1 was demonstrated as a modification of the cogeneration system 100 which becomes a structure shown in FIG. 4, for example, it can apply similarly in the cogeneration system 100 which becomes a structure shown in FIG. 2 or 3. That is, also in the cogeneration system 100 having the configuration shown in FIG. 2 or 3, the ammonia absorption refrigeration machine 10 supplies air to be sent to the SOFC hot module 1 instead of the radiator 54 as shown in FIG. It is good also as a structure provided with the refrigerant
- FIG. 6 is a schematic diagram illustrating an example of the configuration of the cogeneration system 100 according to the second modification of the first embodiment.
- FIG. 6 is the structure similar to the cogeneration system 100 shown in FIG. 4 except the point comprised so that the water of the drain tank 2 can be supplied to the total heat exchanger 7.
- symbol is attached
- FIG. 7 is a schematic diagram illustrating an example of a schematic configuration of the total heat exchanger 7 in the cogeneration system 100 illustrated in FIG. 6.
- the total heat exchanger 7 includes a fuel passage portion 72 through which fuel (raw material) gas passes and a heating portion 71 through which exhaust gas passes.
- the fuel passage portion 72 and the heating portion 71 are separated by a selectively permeable membrane 73 that selectively permeates moisture.
- the condensed water and the exhaust gas are directly brought into contact with each other on the one side of the selectively permeable membrane 73, that is, the heating unit 71 to exchange heat (that is, mix) to produce water vapor. Then, the water vapor and the fuel (raw material) gas passing through the fuel passage 72 are subjected to total heat exchange through the permselective membrane 73. Thereby, fuel (raw material) gas can be heated and humidified.
- Such a heat exchange mode by direct contact type heat exchange and total heat exchange has advantages of high heat exchange efficiency and easy simplification and miniaturization of equipment.
- the temperature of the exhaust gas discharged from the ammonia absorption refrigerator 10 is about 150 ° C., and this exhaust gas has enough energy to vaporize the supplied condensed water. Therefore, in the second modification, the fuel gas can be further humidified by providing the condensed water stored in the drain tank 2 to the total heat exchanger 7.
- the steam (condensed water) mixed with the exhaust gas is further heat-exchanged with the air by the condensation heat exchanger 8 provided at the subsequent stage of the total heat exchanger 7, and condensed to the drain tank 2. To be recovered.
- the ammonia absorption refrigerating machine 10 may include a refrigerant condensing heat exchanger 58 instead of the radiator 54.
- Modification 4 Furthermore, as Modification 4, as shown in FIG. 8, the structure of Modification 3 described above is further added to the fuel check valve 4, the reformed gas check valve 5, and the hydrodesulfurization heat exchanger (reduction reaction section). 6 and a trap (TRAP) (adsorption part) 18 may be provided. And it is set as the structure which performs the desulfurization which was performed with the deflow filter in the fuel processor 3 with the hydrodesulfurization heat exchanger 6.
- FIG. FIG. 8 is a schematic diagram illustrating an example of a schematic configuration of the cogeneration system 100 according to the fourth modification of the first embodiment.
- the configuration of the modified example 4 is the same as the configuration of the modified example 3 except that a fuel check valve 4, a reformed gas check valve 5, a hydrodesulfurization heat exchanger 6, and a trap (TRAP) 18 are newly provided. The same. For this reason, description of members other than these newly provided members is omitted.
- the hydrodesulfurization heat exchanger 6 is capable of removing sulfur compounds contained in the fuel (raw material) gas.
- the exhaust gas flowing through the exhaust gas side passage of the hydrodesulfurization heat exchanger 6 and the fuel gas side stream Heat exchange is performed with the fuel gas flowing through the passage, and desulfurization is performed as follows.
- the hydrodesulfurization heat exchanger 6 reduces the sulfur compound contained in the fuel (raw material) gas using, for example, a copper zinc catalyst to generate hydrogen sulfide. And the hydrogen sulfide produced
- the optimum temperature for heating the fuel (raw material) gas in order to perform this reduction reaction is approximately 250 ° C. to 300 ° C.
- the temperature inside the SOFC hot module 1 is about 650 ° C. to 700 ° C., but the temperature of the exhaust gas discharged from the SOFC hot module 1 is about 250 ° C., and the fuel (raw material) gas is heated to the optimum temperature. I can't.
- the cogeneration system 100 preheats the air supplied to the SOFC hot module 1 by the condensation heat exchanger 8 and the refrigerant condensation heat exchanger 58 and heats and humidifies the fuel (raw material) gas by the total heat exchanger 7.
- the exhaust gas temperature discharged from the SOFC hot module 1 can be set to about 300 ° C. For this reason, it becomes possible to heat a fuel to the above-mentioned optimal reaction temperature by this exhaust gas. Therefore, hydrodesulfurization can be performed with a simple configuration.
- the fuel check valve 4 is provided in the flow path between the fuel processor 3 and the hydrodesulfurization heat exchanger 6, and the reformer 16
- a reformed gas check valve 5 is provided in a flow path between the hydrodesulfurization heat exchanger 6 and the hydrodesulfurization heat exchanger 6.
- a trap (TRAP) 18 is provided downstream of the hydrodesulfurization heat exchanger 6 and between the total heat exchanger 7.
- a part of the hydrogen-rich reformed gas generated by the reformer 16 is drawn out of the SOFC hot module 1 and mixed with fuel (raw material) gas via the reformed gas check valve 5. . That is, a part of the reformed gas supplied to the SOFC cell 13 is diverted so as to go out of the SOFC hot module 1 and mixed with fuel (raw material) gas outside the SOFC hot module 1. Further, the fuel check valve 4 is configured to prevent the backflow of the fuel (raw material) gas.
- the mixed gas is supplied to the hydrodesulfurization heat exchanger 6, heated to the optimum temperature by the exhaust gas flowing in the exhaust gas side passage of the hydrodesulfurization heat exchanger 6, and after the sulfur compound is reduced by the catalyst described above. To be discharged.
- a trap (TRAP) 18 is provided on the downstream side of the hydrodesulfurization heat exchanger 6 and adsorbs hydrogen sulfide generated by the trap (TRAP) 18. All of these members are outside the SOFC hot module 1 and can be easily maintained such as replacement. In addition, since water inhibits the reduction reaction, the order is preferably performed before fuel humidification as shown in FIG.
- a reduction catalyst (not shown) is laid in the fuel side flow path of the hydrodesulfurization heat exchanger 6.
- the refrigerant condensing heat exchanger 58 is omitted according to the optimum temperature range, and a radiator 54 is provided instead.
- any of the plurality of heat exchangers described above can be appropriately combined depending on the constraint conditions, the use environment, and the like.
- the sulfur concentration is extremely small, adsorptive desulfurization is more advantageous, and the hydrodesulfurization heat exchanger 6 may not be necessary. That is, it is not necessary to provide all of the plurality of heat exchangers described above.
- the exhaust gas after heat exchange with the air is cooled by the condensation heat exchanger 8.
- the exhaust gas may be further cooled by the cooler 55 supplied to the cooler 55.
- the cooler 55 obtains the amount of cold necessary for cooling the exhaust gas to a predetermined temperature in addition to the amount of cold necessary for cooling at least the power amplifier unit of the BTS 11. Must be configured.
- the cooler 55 has a function of cooling the exhaust gas to a predetermined temperature and only needs to cover the necessary amount of cold heat.
- the cogeneration system 100 includes, for example, heat exchangers such as the total heat exchanger 7 and the condensation heat exchanger 8, so that the exhaust gas temperature can be raised (exergy can be improved. Point) will be described more specifically.
- the cogeneration system 100 shown in FIG. 4 will be described as an example.
- the cogeneration system 100 can also obtain the necessary water without receiving the supply of water from the outside in the process of operation of the base station (a point that enables the water balance to be independent).
- the base station a point that enables the water balance to be independent.
- the exhaust gas discharged from the SOFC hot module 1 contains battery reaction product water and combustion product water as water vapor.
- This water vapor is not condensed at the generated heat exchanger temperature (about 150 degrees) in the ammonia absorption refrigerator 10 and is discharged from the ammonia absorption refrigerator 10 as water vapor. Then, as described above, by recovering this water and heating and humidifying the fuel gas, it is possible to reduce the amount of reforming water supplied to the vaporizer 15 accordingly.
- the normal operation condition in the SOFC hot module 1 is that the power generation efficiency is 1 kW.
- the temperature of the exhaust gas is about 250 ° C.
- the temperature of the exhaust gas is about 450 ° C. It becomes.
- the temperature of the exhaust gas is 250 ° C.
- the value is between 450 ° C. That is, the temperature of the exhaust gas rises and becomes higher than 250 ° C.
- FIG. 9 is a diagram showing an example of a material balance in reforming efficiency and fuel / oxygen utilization rate in a battery reaction for generating 1 mol of water from 1 mol of hydrogen and 0.5 mol of oxygen in the cogeneration system 100 according to the first embodiment. is there.
- the fuel (raw material) gas and air introduced into the SOFC hot module 1 finally become exhaust gas containing carbon dioxide, water, nitrogen, and oxygen as a composition.
- the water vapor partial pressure at this time is around 65 ° C. as shown in the exhaust gas composition of FIG. 9, and the fuel can be humidified at a dew point of about 60 ° C. by exchanging the total heat (see fuel humidification state).
- the exhaust gas composition 1.48 mol of water is generated from this system, and at this time, the water vapor partial pressure contained in the exhaust gas composition is 24,996 Pa and the dew point is 65 ° C.
- water of 1.48 mol to 0.98 mol of water contained in the exhaust gas composition can be recovered, water self-sustainability can be achieved.
- FIG. 10 is a diagram showing an example of a material balance in reforming efficiency and fuel / oxygen utilization rate in a battery reaction for generating 1 mol of water from 1 mol of hydrogen and 0.5 mol of oxygen in the cogeneration system 100 according to the first embodiment. is there.
- the dew point temperature becomes substantially equal to the exhaust gas temperature discharged from the total heat exchanger 7.
- Preheated air can be supplied into the SOFC hot module 1 by exchanging heat between the exhaust gas and the air supplied to the SOFC hot module 1 by the condensation heat exchanger 8. Thereby, the exhaust gas temperature discharged from the SOFC hot module 1 can be further increased.
- the temperature rise of the exhaust gas obtained as described above is about 20 ° C. when the air arrival temperature is 70 ° C. (normal temperature + 50 ° C.). Therefore, by combining the total heat exchange by the total heat exchanger 7 and the heat exchange by the condensation heat exchanger 8 as described above, and further including the refrigerant condensation heat exchanger 58 as shown in Modification 1, the SOFC The temperature of the exhaust gas discharged from the hot module 1 will exceed 300 ° C.
- the fuel gas can be heated to the above-described optimum reaction temperature by the hydrodesulfurization heat exchanger 6, which is simple. Hydrodesulfurization can be performed with the configuration. Furthermore, since the temperature of the exhaust gas can be increased to exceed 300 ° C., even the exhaust gas after heat exchange by the hydrodesulfurization heat exchanger 6 has sufficient exergy to drive the ammonia absorption refrigerator 10. Can be kept.
- the condensed water of the drain tank 2 may be supplied to the total heat exchanger 7 like the structure which concerns on the modification 2-4, heating of fuel gas by the total heat exchanger 7 and Since the remaining condensed water used after humidification can be recovered by the condensation heat exchanger 8, water necessary for the vaporizer 15 can be covered.
- the reforming water necessary for the reforming reaction is 0.98 mol.
- the exhaust gas is used for driving the ammonia absorption refrigerator 10 in the first stage as described above. Then, the crude heat is transferred from the exhaust gas used in the ammonia absorption refrigerator 10 to a fuel (raw material) gas by the total heat exchanger 7. Finally, the exhaust gas can be cooled to a temperature at which the water balance can be self-supported by heat exchange with air in the condensation heat exchanger 8.
- the cogeneration system 100 includes a plurality of heat exchangers (the total heat exchanger 7 and the condensation heat exchanger 8, and further the refrigerant condensing heat exchanger 58), thereby exhaust gas. Exergy can be increased.
- a regenerative heat exchanger 51 is provided, and the ammonia absorption refrigerator 10 is driven by heating the regenerative heat exchanger 51 with exhaust gas.
- a hydrodesulfurization heat exchanger 6 is provided, and the hydrodesulfurization heat exchanger 6 is heated with exhaust gas to remove sulfur compounds contained in the fuel (raw material) gas, so that the exhaust gas temperature is finally reduced.
- the water balance at the base station can be made independent by lowering the temperature to below 46 ° C.
- the cogeneration system 100 can replace the SOFC system 101 with a base power supply, increase the overall efficiency by cogeneration with the ammonia absorption chiller 10, and can also make the water balance independent. For this reason, even if there is no water source and a base station is installed in a GRID undeveloped area, the operation can be facilitated and the profitability can be improved.
- the SOFC system 101 functioning as a power generator, the BTS (equipment equipment) 11 in the base station shelter that uses the power generated by the SOFC system 101, and the power elements of the power amplifier unit included in the BTS 11 are provided.
- the cogeneration system 100 including the ammonia absorption refrigerator (cooling device, absorption cooling device) 10 for cooling has been described.
- FIG. 11 is a schematic diagram illustrating an example of a schematic configuration of a cogeneration system 100 according to another embodiment (Embodiment 2).
- the configuration of the condensing unit 30 is described as the configuration of the condensing unit 30 illustrated in FIG. 4, but is not necessarily limited thereto.
- the condensation unit 30 provided in the SOFC system 101 according to the second embodiment may be configured as shown in FIGS.
- the cogeneration system 100 is configured such that the ammonia absorption refrigerator 10 cools the exhaust gas instead of cooling the power amplifier section of the BTS 11 to obtain condensed water. That is, the object to be cooled that is cooled by the ammonia absorption refrigerator 10 is further cooled by the condensing unit 30 to be exhaust gas from which condensed water is recovered.
- symbol is attached
- the cogeneration system 100 according to the second embodiment is an alternative to cooling the BTS 11 by the ammonia absorption refrigerator 10. 1 in that the exhaust gas discharged from the condensation heat exchanger 8 is cooled.
- the exhaust gas discharged from the SOFC hot module 1 uses the heat of the exhaust gas in the ammonia absorption refrigerator 10. Used for operation. That is, the ammonia absorption refrigerator 10 cools the exhaust gas discharged from the SOFC hot module 1 by consuming part of the heat of the exhaust gas. As a result, the exhaust gas that has consumed a certain amount of heat undergoes total heat exchange with the fuel (raw material) gas supplied to the SOFC hot module 1 in the total heat exchanger 7. Furthermore, heat is exchanged by the condensation heat exchanger 8 between the exhaust gas after the total heat exchange and the air supplied to the SOFC hot module 1.
- the exhaust gas heat-exchanged by the condensation heat exchanger 8 is supplied to the cooling unit 60 of the ammonia absorption refrigeration machine 10 and further cooled by the cooling unit 60.
- the cogeneration system 100 which concerns on Embodiment 2 can improve the production amount of the condensed water from waste gas.
- the consumption destination of the power generated by the SOFC system 101 is not limited to the base station (BTS 11 in the base station shelter).
- BTS 11 in the base station shelter For example, as shown in FIG.
- a general power load 61 may be used.
- FIG. 12 is a schematic diagram illustrating an example of a schematic configuration of a cogeneration system according to another embodiment (Embodiment 2).
- the SOFC has been described as an example of the power generation device.
- the present invention is not limited to this.
- a molten carbonate fuel cell MCFC
- the fuel cell may be a high-temperature operation type fuel cell that has a high operating temperature of, for example, 400 ° C. or higher and can obtain high-temperature exhaust gas.
- the cogeneration system 100 forcibly cools a member that needs to be cooled efficiently and can make the water balance self-supporting in the system. It is useful as a power source for driving equipment installed in a place.
- the apparatus which consists of a combination of the member which requires forced cooling, and an unnecessary member is not limited to BTS mentioned above,
- power consumption such as a server, a data center, a ship, or communication equipment for broadcasting stations It is a general-purpose configuration as equipment. Therefore, the cogeneration system of the present invention can be applied to these power facilities.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Manufacturing & Machinery (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Fuel Cell (AREA)
- Chimneys And Flues (AREA)
Abstract
Description
図13に示すように、現状の基地局の最も一般的な構成としては、基地局シェルター200、系統電力(GRID;グリッド)201、およびディーゼル発電機(DG)202を備え、基地局シェルター200へは、GRID201とDG202との両系統から電力が供給される構成が挙げられる。図13は現状の基地局の概略構成の一例を示す模式図である。
このため、基地局の消費電力量はBTS211の所要電力よりも基地局シェルター200内の室温に直接的に影響する外気温に依存することとなる。
以下、本発明の好ましい実施の形態(実施形態1)を、図面を参照して説明する。なお、以下では全ての図を通じて同一又は対応する構成部材には同一の参照符号を付して、その説明については省略する。
図1を参照して本実施の形態(実施形態1)に係る基地局において実現されているコージェネレーションシステム100の一例について説明する。図1は実施形態1に係る基地局におけるコージェネレーションシステム100の概略構成の一例を示す模式図である。
ここで実施形態1に係るコージェネレーションシステム100が備えるSOFCシステム101について説明する。SOFCシステム101は、燃料電池としてSOFC(固体酸化物型燃料電池)を利用した発電システムである。SOFCシステム101は、図1に示すように、SOFCホットモジュール1、ドレインタンク2、燃料処理器(FPS)3、凝縮ユニット30、ブロワー9、および第1凝縮水ポンプ20を備える。
ここで、SOFCシステム101が備える凝縮ユニット30の構成の一例について図2を参照して説明する。図2は、実施形態1に係る基地局におけるコージェネレーションシステム100の概略構成の一例を示す模式図である。
次に、上述した図4に示す構成を有するSOFCシステム101を例に挙げ、基本的な動作を説明する。
H2+1/2O2 → H2O ・・・(1)
この反応は水素の燃焼反応と同様である。この燃焼反応で得られる燃焼エネルギーに相当するエネルギーを電気化学的に取り出すのが燃料電池の基本原理である。この反応によって発電を行うと同時に発熱するが、この発熱により生じる熱(発電廃熱)も気化器15の水蒸発エネルギーおよび改質器16の改質反応エネルギーの一部として利用される。ここで実施形態1に係るSOFCホットモジュール1を近年主流のアノード支持方SOFCとした場合、その電池運転温度は700℃程度となる。
ここで、上述したSOFCシステム101に供給する原料(燃料)ガスについて説明する。一般的には原料(燃料)ガスとしてLNG(Liquefied natural gas;液化天然ガス)ないしLPG(liquefied petroleum gas;液化石油ガス)が用いられている。これらのガスは液化される段階で自動的に不純物が除去され極めて高純度なものとなり、安全性の観点から一定量の腐臭剤が添加されて供給される。腐臭剤は硫黄化合物が主流であるが、硫黄は広範な触媒に対する触媒毒となる。また、地域によってはガス田供給の天然ガスを原料(燃料)ガスとしてSOFCシステム101にパイプライン供給する場合がある。この場合、ガスは炭化水素のほか一定量の硫黄分を含んでいる。さらに、原料(燃料)ガスとして硝化ガス(バイオガス)を利用する場合、硝化ガスには種々の臭気物質が含まれる。
次に、実施形態1に係るコージェネレーションシステム100が熱負荷として備えるアンモニア吸収式冷凍機10の構成について説明する。このアンモニア吸収式冷凍機10は、図4に示すように、再生熱交換器51、精留器52、ラジエータ54、吸収器56、および貯留器57を備え、吸収液として水を、冷媒としてアンモニアを使用する。つまり。アンモニア吸収式冷凍機10は、アンモニアおよび水混合媒体を作動流体とする。
次に、実施形態1に係るコージェネレーションシステム100が電力負荷として備えるBTS11について説明する。
続いて、上述したBTS11で消費される消費電力について説明する。BTS11で消費される消費電力は上述したように通信量に依存しており、消費電力が最大で800Wであっても使用時の平均出力に換算すると400W程度となる。このため、SOFCセル13により発電される電力の最大出力を必ずしも800Wとなるように設計する必要はない。例えばSOFCセル13の最大出力を平均出力よりもやや高めの500Wに設計し、平均出力時にはここから得られる電力の余剰分をSB19に貯蔵する構成とする。さらには、アンモニア吸収式冷凍機10によってパワーアンプ部を冷却する温度を35℃よりもさらに過剰に冷却しておく構成とする。
次に、図4に示すコージェネレーションシステム100を例に挙げ、コージェネレーションシステム100における発生電熱比のコントロールについて説明する。上述したように、BTS11の発生電熱比の値は、最大出力時では800W(発生電力):180W(発生熱量)、すなわち約4となる。発生電熱比の値4で180W分の熱量に対応する冷熱を得るように構成することでコージェネレーションシステム100では、電力と冷熱との需給を釣り合わせることができる。
図4に示すように、実施形態1に係るコージェネレーションシステム100が備えるアンモニア吸収式冷凍機10は、発生した冷媒蒸気(気化したアンモニア)を凝縮して液化させるためにラジエータ54を用いて冷却する構成であった。しかしながら図5に示すようにこのラジエータ54の代わりに、SOFCホットモジュール1に送出する空気を供給し、この空気と冷媒蒸気との間で熱交換を行なう冷媒凝縮熱交換器(第4熱交換器)58を備える構成としてもよい。図5は実施形態1の変形例1に係るコージェネレーションシステム100の概略構成の一例を示す図である。なお、ラジエータ54を冷媒凝縮熱交換器58に代えた点を除けば、図4に示すコージェネレーションシステム100と同様な構成であるため、他の部材には同じ符号を付しその説明を省略する。
また、図4に示すコージェネレーションシステム100では、全熱交換器7には燃料(原料)ガスと排ガスとが供給される構成であった。しかしながら、変形例2として図6に示すように、第2凝縮水ポンプ(水輸送部)21を備え、該第2凝縮水ポンプ21によってドレインタンク2の凝縮水を全熱交換器7にさらに供給するように構成してもよい。図6は実施形態1の変形例2に係るコージェネレーションシステム100の構成の一例を示す模式図である。なお、ドレインタンク2の水を全熱交換器7に供給できるように構成されている点を除けば、図4に示すコージェネレーションシステム100と同様な構成である。このため、変形例2に示すコージェネレーションシステム100において備える各部材には同じ符号を付しその説明を省略する。
さらにまた、変形例2に係るコージェネレーションシステム100において、変形例1と同様に、アンモニア吸収式冷凍機10がラジエータ54の代わりに、冷媒凝縮熱交換器58を備えた構成としてもよい。
さらにまた、変形例4として、図8に示すように、上述した変形例3の構成に、さらに燃料逆止弁4、改質ガス逆止弁5、水添脱硫熱交換器(還元反応部)6、およびトラップ(TRAP)(吸着部)18をさらに備えた構成としてもよい。そして、燃料処理器3内の脱流フィルターで行なっていた脱硫を水添脱硫熱交換器6により行なう構成とする。図8は、実施形態1の変形例4に係るコージェネレーションシステム100の概略構成の一例を示す模式図である。
近年の基地局向けBTSには、特に気温の高い地域においてエアコン等の空調機器の電力を不要化するために、パワーアンプにヒートパイプを敷設して外部放熱するタイプのものが存在し、この場合にはパワーアンプは冷熱を必要としないため、冷却器55は、排ガスを所定の温度まで冷却する機能があって必要冷熱量が賄えればよい。
次に、コージェネレーションシステム100が、例えば、全熱交換器7、凝縮熱交換器8等の熱交換器を備えることで、排ガス温度を上昇させることができる点(エクセルギーを向上させることができる点)についてより具体的に説明する。具体的には、図4に示すコージェネレーションシステム100を例に挙げて説明する。
なお、実施形態1では、発電装置として機能するSOFCシステム101と、SOFCシステム101で発電した電力を利用する基地局シェルター内のBTS(設備機器)11と、BTS11が備えるパワーアンプ部の電力素子を冷却するためのアンモニア吸収式冷凍機(冷却装置、吸収式冷却装置)10とを備えたコージェネレーションシステム100について説明した。
2 ドレインタンク
3 燃料処理器
4 燃料逆止弁
5 改質ガス逆止弁
6 水添脱硫熱交換器
7 全熱交換器
8 凝縮熱交換器
9 ブロワー
10 アンモニア吸収式冷凍機
11 BTS
12 パワーマネジメントシステム(PMS)
13 SOFCセル
14 燃焼部
15 気化器
16 改質器
17 集電部材
18 トラップ
20 第1凝縮水ポンプ
21 第2凝縮水ポンプ
22 アノード
23 カソード
51 再生熱交換器
52 精留器
54 ラジエータ
55 冷却器
56 吸収器
57 貯留器
58 冷媒凝縮熱交換器
60 冷却部
61 電力負荷
71 加熱部
72 原料通路部
72 燃料通路部
73 選択透過膜
100 コージェネレーションシステム
101 SOFCシステム
200 基地局シェルター
201 GRID
202 ディーゼル発電機
211 BTS
212 エアコン
213 パワーマネジメントシステム(PMS)
Claims (14)
- 供給された燃料と空気とを利用して発電反応により発電する高温動作型燃料電池セルと、
前記高温動作型燃料電池セルで生じる発電反応熱および未利用の燃料の燃焼熱を利用して改質反応により、供給された原料ガス及び水蒸気から前記燃料となる改質ガスを生成する改質器と、
前記発電反応熱および前記燃焼熱を利用して前記改質器に供給される原料ガスに添加する前記水蒸気を生成するための気化器と、
前記改質器および前記気化器によって利用されて残った、前記発電反応熱および前記燃焼熱を保有する排ガスの熱の一部を消費して被冷却対象物を冷却するとともに、熱の一部を消費することで該排ガスを冷却する冷却装置と、
前記冷却装置により、保有する熱の一部が消費された後の排ガスをさらに冷却し、当該排ガス中に含まれる水分を凝縮させて凝縮水を生成する凝縮ユニットと、を備えるコージェネレーションシステム。 - 前記凝縮ユニットは、前記冷却装置により熱の一部が消費された後の排ガスの熱を利用して、前記気化器に供給する前記原料ガスを加熱する第1熱交換器と、
前記第1熱交換器により熱利用された後の排ガスの熱をさらに利用して、前記固体酸化型燃料電池セルに供給する空気を加熱するとともに、当該排ガス中に含まれる水分を凝縮させて凝縮水を生成する第2熱交換器と、を備える請求項1に記載のコージェネレーションシステム。 - 前記第1熱交換器は、前記冷却装置により熱の一部が消費された後の排ガスの熱を利用して、前記気化器に供給する前記原料ガスを加熱するとともに、排ガス中に含まれる水分により加湿する全熱交換器である請求項2に記載のコージェネレーションシステム。
- 前記凝縮ユニットは、前記冷却装置により熱の一部が消費された後の排ガスを空冷により冷却するための送風機を備え、
前記送風機により前記排ガスを冷却し、当該排ガス中に含まれる水分を凝縮させて凝縮水を生成する請求項1に記載のコージェネレーションシステム。 - 前記気化器は、前記発電反応熱および前記燃焼熱を利用して前記凝縮水を蒸発させることによって前記水蒸気を生成するよう構成されている、請求項1から4のいずれか1項に記載のコージェネレーションシステム。
- 前記冷却装置は、冷媒を吸収液に吸収させて循環させる吸収式冷却装置であって、
前記冷媒の方が吸収液よりも沸点温度が低くなっており、
前記冷媒を吸収した吸収液から該冷媒を分離させるために、前記排ガスと冷媒を吸収した吸収液との間で熱交換する第3熱交換器を備え、該第3熱交換器による熱交換によって得た熱により該冷媒を吸収した吸収液を気化させるよう構成されている、請求項1から5のいずれか1項に記載のコージェネレーションシステム。 - 前記吸収式冷却装置は、気化された、前記冷媒を吸収した吸収液からこの吸収液のみを液化させて冷媒と分離させる精留器と、
前記精留器によって前記吸収液から分離された、気化された冷媒を液化するために、この気化された冷媒と、前記固体酸化型燃料電池セルに供給する空気との間で熱交換を行なう第4熱交換器とを備え、
前記第4熱交換器による、気化された冷媒との熱交換により加熱された空気を高温動作型燃料電池セルに供給する請求項6に記載のコージェネレーションシステム。 - 前記第2熱交換器によって排ガス中から凝縮された凝縮水を、前記第1熱交換器に輸送する水輸送部を備え、
前記水輸送部によって輸送された凝縮水と前記排ガスとを混合して該凝縮水を水蒸気として含む排ガスを生成し、前記第1熱交換器によりこの排ガス中に含まれる水蒸気を前記原料ガスに移動させて当該原料ガスを加熱および加湿するよう構成されている、請求項3に記載のコージェネレーションシステム。 - 前記改質器において生成された改質ガスの一部を分流させて前記原料ガスと混合させた混合ガスから原料ガスに含まれる硫黄化合物を還元して硫化水素を生成する還元反応部と、
前記還元反応部により生成した硫化水素を吸着除去する吸着部と、を備え、
前記還元反応部には、さらに前記冷却装置に供給する排ガスが供給されており、当該排ガスから伝達される熱により前記還元反応部における反応温度を維持する請求項8に記載のコージェネレーションシステム。 - 前記高温動作型燃料電池セルにより発電した電力を蓄電する蓄電装置を備える請求項1から9のいずれか1項に記載のコージェネレーションシステム。
- 前記冷却装置は、前記高温動作型燃料電池セルにより発電された電力によって稼動する設備機器において、冷却が必要な冷却必要部材を前記冷却被対象物として少なくとも冷却する請求項1から10のいずれか1項に記載のコージェネレーションシステム。
- 前記冷却必要部材を冷却するべき温度の上限値が定められており、
前記冷却装置は、冷却必要部材を前記定められた上限値よりもさらに低い温度となるように冷却する請求項11に記載のコージェネレーションシステム。 - 前記冷却必要部材の温度情報に基づき、前記高温動作型燃料電池セルの発電量が制御される請求項11または12に記載のコージェネレーションシステム。
- 前記冷却装置は、前記冷却被対象物として、前記凝縮ユニットによって冷却された排ガスをさらに冷却し、該ガス中に含まれる水分をさらに凝縮させて凝縮水を生成する請求項1から10のいずれか1項に記載のコージェネレーションシステム。
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2012555248A JP5209153B1 (ja) | 2011-09-06 | 2012-09-05 | コージェネレーションシステム |
US13/821,880 US9318761B2 (en) | 2011-09-06 | 2012-09-05 | Cogeneration system |
EP12829137.4A EP2755269B1 (en) | 2011-09-06 | 2012-09-05 | Cogeneration system |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2011-194090 | 2011-09-06 | ||
JP2011194090 | 2011-09-06 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013035312A1 true WO2013035312A1 (ja) | 2013-03-14 |
Family
ID=47831783
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2012/005606 WO2013035312A1 (ja) | 2011-09-06 | 2012-09-05 | コージェネレーションシステム |
Country Status (4)
Country | Link |
---|---|
US (1) | US9318761B2 (ja) |
EP (1) | EP2755269B1 (ja) |
JP (1) | JP5209153B1 (ja) |
WO (1) | WO2013035312A1 (ja) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014167764A1 (ja) * | 2013-04-11 | 2014-10-16 | パナソニック株式会社 | 燃料電池システム |
JP2015135812A (ja) * | 2013-12-19 | 2015-07-27 | パナソニック株式会社 | 燃料電池システム |
JP5886483B1 (ja) * | 2014-05-21 | 2016-03-16 | パナソニック株式会社 | 固体酸化物形燃料電池システム及びその停止方法 |
JP5926866B2 (ja) * | 2014-05-28 | 2016-05-25 | パナソニック株式会社 | 固体酸化物形燃料電池システム及びその停止方法 |
WO2023105890A1 (ja) * | 2021-12-06 | 2023-06-15 | 株式会社日立製作所 | 水素混焼用電子制御装置及びそれを用いた発電システム |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015075890A1 (ja) * | 2013-11-20 | 2015-05-28 | パナソニックIpマネジメント株式会社 | 燃料電池システム |
SG2013095864A (en) * | 2013-12-26 | 2015-07-30 | Cyclect Electrical Engineering Pte Ltd | Cogeneration plant |
US9546575B2 (en) | 2014-11-19 | 2017-01-17 | International Business Machines Corporation | Fuel vaporization using data center waste heat |
AT522388B1 (de) | 2019-04-08 | 2021-08-15 | Avl List Gmbh | Brennstoffzellensystem mit Absorptionskältemaschine |
CN114765266A (zh) * | 2021-01-14 | 2022-07-19 | 清华大学 | 一种提高热效率并优化水管理的sofc热电联供系统 |
CN115939445B (zh) * | 2023-03-01 | 2023-05-26 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | 一种高效固体氧化物燃料电池热电联产系统及联产方法 |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH04126369A (ja) * | 1990-09-17 | 1992-04-27 | Tokyo Gas Co Ltd | 燃料電池における原燃料改質用水蒸気源の自給システム |
JP2006073416A (ja) | 2004-09-03 | 2006-03-16 | Kansai Electric Power Co Inc:The | 吸収式冷凍機複合型燃料電池システム |
JP2008293749A (ja) * | 2007-05-23 | 2008-12-04 | Daikin Ind Ltd | 燃料電池駆動式冷凍装置 |
JP2009168348A (ja) * | 2008-01-16 | 2009-07-30 | Toyota Motor Corp | 熱電併給装置およびその制御方法 |
JP2010218691A (ja) * | 2009-03-13 | 2010-09-30 | Hitachi Computer Peripherals Co Ltd | 燃料電池電源システムおよびその制御方法 |
US8005510B2 (en) | 2008-07-10 | 2011-08-23 | T-Mobile Usa, Inc. | Cell site power conservation |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6054229A (en) * | 1996-07-19 | 2000-04-25 | Ztek Corporation | System for electric generation, heating, cooling, and ventilation |
US8241801B2 (en) * | 2006-08-14 | 2012-08-14 | Modine Manufacturing Company | Integrated solid oxide fuel cell and fuel processor |
GB0621784D0 (en) * | 2006-11-01 | 2006-12-13 | Ceres Power Ltd | Fuel cell heat exchange systems and methods |
JP2010257644A (ja) * | 2009-04-22 | 2010-11-11 | Honda Motor Co Ltd | 燃料電池システムの制御方法 |
-
2012
- 2012-09-05 WO PCT/JP2012/005606 patent/WO2013035312A1/ja active Application Filing
- 2012-09-05 US US13/821,880 patent/US9318761B2/en not_active Expired - Fee Related
- 2012-09-05 EP EP12829137.4A patent/EP2755269B1/en not_active Not-in-force
- 2012-09-05 JP JP2012555248A patent/JP5209153B1/ja active Active
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH04126369A (ja) * | 1990-09-17 | 1992-04-27 | Tokyo Gas Co Ltd | 燃料電池における原燃料改質用水蒸気源の自給システム |
JP2006073416A (ja) | 2004-09-03 | 2006-03-16 | Kansai Electric Power Co Inc:The | 吸収式冷凍機複合型燃料電池システム |
JP2008293749A (ja) * | 2007-05-23 | 2008-12-04 | Daikin Ind Ltd | 燃料電池駆動式冷凍装置 |
JP2009168348A (ja) * | 2008-01-16 | 2009-07-30 | Toyota Motor Corp | 熱電併給装置およびその制御方法 |
US8005510B2 (en) | 2008-07-10 | 2011-08-23 | T-Mobile Usa, Inc. | Cell site power conservation |
JP2010218691A (ja) * | 2009-03-13 | 2010-09-30 | Hitachi Computer Peripherals Co Ltd | 燃料電池電源システムおよびその制御方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2755269A4 * |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014167764A1 (ja) * | 2013-04-11 | 2014-10-16 | パナソニック株式会社 | 燃料電池システム |
JP5870320B2 (ja) * | 2013-04-11 | 2016-02-24 | パナソニックIpマネジメント株式会社 | 燃料電池システム |
JP2015135812A (ja) * | 2013-12-19 | 2015-07-27 | パナソニック株式会社 | 燃料電池システム |
US10461341B2 (en) | 2013-12-19 | 2019-10-29 | Panasonic Corporation | Fuel cell system |
JP5886483B1 (ja) * | 2014-05-21 | 2016-03-16 | パナソニック株式会社 | 固体酸化物形燃料電池システム及びその停止方法 |
US10096851B2 (en) | 2014-05-21 | 2018-10-09 | Panasonic Corporation | Solid oxide fuel cell system and method of stopping the same |
JP5926866B2 (ja) * | 2014-05-28 | 2016-05-25 | パナソニック株式会社 | 固体酸化物形燃料電池システム及びその停止方法 |
US10079396B2 (en) | 2014-05-28 | 2018-09-18 | Panasonic Corporation | Solid-oxide fuel cell system and method of stopping same |
WO2023105890A1 (ja) * | 2021-12-06 | 2023-06-15 | 株式会社日立製作所 | 水素混焼用電子制御装置及びそれを用いた発電システム |
Also Published As
Publication number | Publication date |
---|---|
US20130273445A1 (en) | 2013-10-17 |
EP2755269A4 (en) | 2015-04-29 |
US9318761B2 (en) | 2016-04-19 |
EP2755269B1 (en) | 2016-08-17 |
JP5209153B1 (ja) | 2013-06-12 |
EP2755269A1 (en) | 2014-07-16 |
JPWO2013035312A1 (ja) | 2015-03-23 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP5209153B1 (ja) | コージェネレーションシステム | |
CA2668007C (en) | Fuel cell heat exchange system with burner arrangement | |
US8304123B2 (en) | Ambient pressure fuel cell system employing partial air humidification | |
KR100910429B1 (ko) | 연료전지 발전시스템의 폐열을 이용한 흡수식 냉난방시스템 및 방법 | |
WO2014167764A1 (ja) | 燃料電池システム | |
JP5625368B2 (ja) | 冷凍機複合型燃料電池システム | |
JP2013229203A (ja) | 固体酸化物形燃料電池システム | |
CN102456897B (zh) | 燃料电池电热冷联供系统 | |
KR101339672B1 (ko) | 연료전지의 열을 이용한 냉난방 공급시스템 | |
CN108352550A (zh) | 带冷凝-蒸发装置燃料电池系统并行冷凝蒸发方法和装置及带冷凝-蒸发装置染料电池系统 | |
JP2005337516A (ja) | ハイブリッド給湯システム及びその運転方法 | |
AU2003236384A1 (en) | Humidification of Reactant Streams in Fuel Cells | |
JP2004211979A (ja) | 吸収冷凍システム | |
JP2013239404A (ja) | 固体酸化物形燃料電池システム | |
JP2003031255A (ja) | 燃料電池発電装置、及び凝縮水の貯水タンクへの供給方法 | |
WO2013171980A1 (ja) | 燃料電池システム | |
JP6405538B2 (ja) | 燃料電池システム | |
JP3956208B2 (ja) | 燃料電池発電システムとその運転方法 | |
AU2007315974B2 (en) | Fuel cell heat exchange systems and methods | |
GB2458112A (en) | Heat and Process Water Recovery System | |
JP4470329B2 (ja) | 燃料電池発電装置およびその運転方法 | |
JP2009170189A (ja) | 燃料電池システム及び燃料電池システムにおける凝縮水の回収方法 | |
JP2010181063A (ja) | 熱電併給システム | |
KR100915267B1 (ko) | 연료전지 발전시스템을 이용한 흡수식 냉방 시스템 및 방법 | |
JP2005251759A (ja) | 固体高分子型燃料電池システム |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
ENP | Entry into the national phase |
Ref document number: 2012555248 Country of ref document: JP Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 13821880 Country of ref document: US |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 12829137 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
REEP | Request for entry into the european phase |
Ref document number: 2012829137 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2012829137 Country of ref document: EP |