WO2015019886A1 - Dispositif de récupération de chaleur perdue - Google Patents

Dispositif de récupération de chaleur perdue Download PDF

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Publication number
WO2015019886A1
WO2015019886A1 PCT/JP2014/069827 JP2014069827W WO2015019886A1 WO 2015019886 A1 WO2015019886 A1 WO 2015019886A1 JP 2014069827 W JP2014069827 W JP 2014069827W WO 2015019886 A1 WO2015019886 A1 WO 2015019886A1
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WO
WIPO (PCT)
Prior art keywords
waste heat
working fluid
heat recovery
heat exchanger
exhaust
Prior art date
Application number
PCT/JP2014/069827
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English (en)
Japanese (ja)
Inventor
加藤　剛
泰英 岡▲崎▼
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日立造船株式会社
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Publication of WO2015019886A1 publication Critical patent/WO2015019886A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N5/00—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy
    • F01N5/02—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy the devices using heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/065—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle the combustion taking place in an internal combustion piston engine, e.g. a diesel engine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02G—HOT GAS OR COMBUSTION-PRODUCT POSITIVE-DISPLACEMENT ENGINE PLANTS; USE OF WASTE HEAT OF COMBUSTION ENGINES; NOT OTHERWISE PROVIDED FOR
    • F02G5/00—Profiting from waste heat of combustion engines, not otherwise provided for
    • F02G5/02—Profiting from waste heat of exhaust gases
    • 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
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the present invention relates to a waste heat recovery apparatus.
  • a waste heat recovery apparatus that recovers energy from waste heat of a prime mover or the like using a Rankine cycle.
  • an apparatus that performs an organic Rankine cycle (ORC) using an organic medium as a working fluid is used.
  • ORC organic Rankine cycle
  • a low boiling point organic medium such as hydrofluorocarbon (HFC) -based R245fa or R365mfc used as a refrigerant for a refrigeration apparatus or the like is used as a medium for the waste heat recovery apparatus.
  • HFC hydrofluorocarbon
  • R245fa As a medium in a geothermal heat recovery apparatus.
  • high-purity R245fa starts thermal decomposition in about 31 hours in a test conducted at a temperature of 330 ° C. (330 degrees Celsius).
  • R365mfc and the like also start thermal decomposition in several tens of hours under the condition of about 200 ° C.
  • a silicon-based organic medium such as octamethylsiloxane (OMTS) is used in a waste heat recovery apparatus that recovers energy from waste heat of 300 ° C. or higher.
  • heat medium oil thermal oil
  • energy recovery is performed by first heating the heat medium oil using waste heat as a heat source, and then performing ORC using the heat medium oil as a heat source and OMTS as a working fluid. Therefore, the energy recovery efficiency is lower than a waste heat recovery apparatus that does not use an intermediate medium, that is, a waste heat recovery apparatus that directly heats the ORC medium using waste heat.
  • heat-medium oil and OMTS have combustibility, very advanced management is needed in order to use a waste-heat recovery apparatus stably.
  • the present invention is directed to a waste heat recovery device, and aims to efficiently and stably recover waste heat from a relatively high temperature heat source.
  • the waste heat recovery apparatus uses a waste heat from the apparatus as a heat source to heat R4310mee, which is a working fluid, and expands the working fluid heated by the heat exchanger to obtain mechanical energy.
  • An expander to be recovered a condenser that condenses and liquefies the working fluid expanded by the expander, and a pump that sends the working fluid liquefied by the condenser to the heat exchanger.
  • the working fluid led from the heat exchanger to the expander is in a supercritical state.
  • the device is a prime mover
  • the heat source is an exhaust of the prime mover
  • another heat exchanger that is disposed between the pump and the heat exchanger and that heats the working fluid delivered from the pump using a pressurized intake air supplied to the prime mover as a heat source. Further prepare.
  • the apparatus further includes a regenerator that heats the working fluid guided from the other heat exchanger to the heat exchanger.
  • FIG. 1 is a diagram showing a configuration of a prime mover system 1 according to a first embodiment of the present invention.
  • the prime mover system 1 is used as a power generation system of a power plant, for example.
  • the motor system 1 includes a motor 2 with a supercharger and a waste heat recovery device 6 that recovers waste heat of the motor 2 with a supercharger.
  • the prime mover 2 with a supercharger includes a prime mover 3 that is an internal combustion engine and a supercharger 4 that is a turbocharger.
  • the prime mover 3 is, for example, a four-cycle gas engine having a maximum output (100% output) of about 6000 kW.
  • the supercharger 4 includes a turbine 41 and a compressor 42 that is mechanically connected to the turbine 41.
  • the prime mover 3 and the supercharger 4 are connected by an air supply path 31 and an exhaust path 32.
  • the exhaust path 32 guides the exhaust from the prime mover 3 to the turbine 41 and guides the exhaust that has passed through the turbine 41 to the outside of the prime mover system 1.
  • the turbine 41 is rotated by the exhaust gas supplied from the prime mover 3 through the exhaust passage 32.
  • the exhaust used for the rotation of the turbine 41 is discharged to the outside of the prime mover system 1 through the exhaust path 31.
  • the compressor 42 uses the rotational force generated in the turbine 41 (that is, using the rotation of the turbine 41 as power), and the intake air (from the outside of the prime mover system 1 to the supercharger 4 via the intake passage 43). Pressurize and compress air). Compressed air (hereinafter referred to as “supply air”) pressurized by the compressor 42 is cooled by a compressed air heat exchanger 621 (described later) provided on the air supply path 31 and then the prime mover. 3 is supplied.
  • the air supply path 31 is a flow path that guides pressurized intake air from the supercharger 4 to the prime mover 3, that is, a pressurized intake path.
  • the waste heat recovery apparatus 6 includes a pipe 61, an exhaust heat exchanger 622, an expander 63, a condenser 64, and a pump 65.
  • the exhaust heat exchanger 622, the expander 63, the condenser 64, and the pump 65 are connected in the above order by a pipe 61 through which R4310mee as a working fluid flows.
  • R4310mee is an organic medium that has thermal stability even at a relatively high temperature range of about 500 ° C. (about 500 degrees Celsius) (ie, hardly undergoes thermal decomposition under conditions of about 500 ° C.).
  • R4310mee is a nonflammable fluid.
  • ORC organic Rankine cycle
  • the liquid working fluid (that is, R4310mee) is pressurized by the pump 65 and sent to the exhaust heat exchanger 622.
  • the pressure of the working fluid delivered from the pump 65 is lower than the critical pressure of the working fluid.
  • the critical pressure means the pressure at the critical point of the working fluid (that is, the limit point of the temperature and pressure range where the phase transition between the gas phase and the liquid phase of the working fluid can occur).
  • the critical pressure of R4310mee is about 2.29 MPa (megapascal).
  • the exhaust heat exchanger 622 is provided on the exhaust path 32 on the downstream side of the turbine 41.
  • the liquid working fluid sent from the pump 65 is heated using the exhaust from the turbine 41 flowing through the exhaust passage 32 (that is, the exhaust from the prime mover 3 after passing through the turbine 41) as a heat source.
  • the working fluid is heated using the waste heat of the supercharger-equipped prime mover 2 included in the exhaust as a heat source.
  • the temperature of the exhaust gas flowing into the exhaust heat exchanger 622 is about 420 ° C., for example. Even if the output of the prime mover 3 fluctuates, the exhaust temperature does not fluctuate significantly.
  • the exhaust heat exchanger 622 includes a preheater 623 and an evaporator 624.
  • the liquid working fluid is heated by the exhaust flowing through the exhaust path 32.
  • the liquid working fluid heated by the preheater 623 is guided to the evaporator 624.
  • the evaporator 624 the liquid working fluid is heated by the exhaust flowing through the exhaust path 32 and is vaporized (evaporates).
  • the working fluid vaporized in the exhaust heat exchanger 622 is in a saturated steam state, for example, and is guided to the expander 63.
  • the working fluid may be heated to a superheated steam state.
  • the expander 63 expands the working fluid heated and vaporized by the exhaust heat exchanger 622 and recovers mechanical energy.
  • a turbine that is rotated by a working fluid is used as the expander 63.
  • the shaft of the turbine is connected to the generator 8, and the generator 8 generates power when the turbine is driven by the working fluid sent from the exhaust heat exchanger 622 via the pipe 61.
  • FIG. 2 is a TS diagram of the waste heat recovery device 6.
  • the horizontal axis of FIG. 2 indicates specific entropy, and the vertical axis indicates temperature.
  • a solid line 901 in FIG. 2 indicates the ORC in the waste heat recovery apparatus 6.
  • broken lines 902 and 903 in FIG. 2 are a saturated liquid line and a saturated vapor line of R4310mee, which is a working fluid of the waste heat recovery apparatus 6, respectively.
  • the saturated vapor line 903 of R4310mee has a positive gradient on the TS diagram.
  • the expander 63 when the working fluid in the saturated vapor state corresponding to the point 904 in FIG. 2 expands, the working fluid in the dry vapor state corresponding to the point 905 in FIG. 2 is obtained. Accordingly, the generation of droplets of the working fluid in the expander 63 is prevented (or suppressed).
  • the gaseous working fluid that has passed through the expander 63 shown in FIG. 1 is guided to the condenser 64.
  • the condenser 64 condenses and liquefies the working fluid expanded by the expander 63.
  • the working fluid liquefied by the condenser 64 is pressurized by the pump 65 and sent to the exhaust heat exchanger 622.
  • FIG. 3 is a diagram showing the recovery power in the waste heat recovery device 6 of the prime mover system 1 shown in FIG.
  • the horizontal axis in FIG. 3 indicates the temperature of the working fluid flowing from the exhaust heat exchanger 622 to the expander 63. Hereinafter, this temperature is referred to as “expander inlet temperature”.
  • the vertical axis in FIG. 3 indicates the recovery power ratio that is a dimensionless value of the recovery power of the waste heat recovery device 6.
  • the recovery power ratio is obtained by dividing the recovery power of the waste heat recovery device 6 corresponding to each expander inlet temperature by the recovery power of the waste heat recovery device 6 when the expander inlet temperature is 120 ° C.
  • the recovery power of the waste heat recovery device 6 corresponding to each expander inlet temperature is calculated by assuming that the working fluid heated to the saturated steam state in the exhaust heat exchanger 622 flows into the expander 63.
  • FIG. 4 is a diagram showing the evaporating pressure of the working fluid in the waste heat recovery apparatus 6 when calculating each recovery power ratio in FIG.
  • the horizontal axis of FIG. 4 shows the expander inlet temperature of the working fluid, and the vertical axis shows the evaporation pressure of the working fluid.
  • the recovery power ratio and the evaporation pressure at each expander inlet temperature of the waste heat recovery apparatus 6 are indicated by solid circles, respectively.
  • the waste heat recovery apparatus of the first comparative example has the same configuration as the waste heat recovery apparatus 6 shown in FIG.
  • R245fa is used as the working fluid instead of R4310mee. 3 and 4
  • the recovery power ratio and the evaporation pressure at each expander inlet temperature of the waste heat recovery apparatus of the first comparative example are indicated by hollow triangles, respectively.
  • the recovery power in the waste heat recovery apparatus of the first comparative example is also calculated by assuming that R245fa heated to the saturated steam state in the exhaust heat exchanger flows into the expander. Desired.
  • the structure of each structure can be simplified compared with the waste heat recovery apparatus of a 1st comparative example, and manufacturing cost can be reduced. Further, the waste heat recovery apparatus 6 can facilitate the operation and management of the apparatus as compared with the waste heat recovery apparatus of the first comparative example.
  • FIG. 5 is a diagram showing the relationship between the expander inlet temperature and the recovery power in the waste heat recovery apparatus 6 shown in FIG.
  • the horizontal axis in FIG. 5 indicates the expander inlet temperature
  • the vertical axis indicates the recovery power ratio.
  • the recovered power ratio is obtained by dividing the recovered power corresponding to each expander inlet temperature by the recovered power when the expander inlet temperature is 190 ° C.
  • the recovery power in the waste heat recovery device 6 increases. In other words, when the expander inlet temperature increases, the waste heat recovery efficiency of the waste heat recovery device 6 can be improved.
  • the temperature of the exhaust gas flowing into the exhaust heat exchanger 622 is about 420 ° C., for example. Therefore, the working fluid can be easily heated to a relatively high temperature (for example, 300 ° C. or 350 ° C.) in the exhaust heat exchanger 622 and supplied to the expander 63. In other words, the expander inlet temperature can be easily made relatively high.
  • the working fluid R245fa is thermally decomposed in a relatively short time in a high temperature range (for example, a temperature range higher than 300 ° C.). It is difficult to recover waste heat stably.
  • the working fluid R4310mee has thermal stability even at about 500 ° C. as described above. Therefore, the waste heat can be efficiently and stably recovered from the exhaust of the prime mover 3, which is a relatively high-temperature heat source.
  • the R4310mee recovers the waste heat directly from the exhaust without passing through the intermediate medium in the exhaust heat exchanger 622. For this reason, waste heat is once recovered from exhaust gas with a heat transfer oil (thermal oil) as an intermediate medium, and ORC using a silicon-based organic medium such as octamethylsiloxane (OMTS) as a working fluid using the heat transfer oil as a heat source.
  • a waste heat recovery apparatus that performs the above (hereinafter referred to as “waste heat recovery apparatus of another comparative example”), exhaust heat of exhaust can be recovered efficiently.
  • the heat transfer oil that is an intermediate medium and the OMTS that is the working fluid of the ORC are flammable, so that they are extremely advanced in order to use the apparatus stably. Management is required.
  • R4310mee which is a working fluid of the waste heat recovery device 6, is a non-flammable fluid, and thus the waste heat recovery device 6 has high safety. Therefore, management of the waste heat recovery device 6 can be simplified.
  • the exhaust heat of the prime mover 3 can be efficiently recovered by heating the working fluid by the exhaust of the relatively high temperature prime mover 3 in the exhaust heat exchanger 622.
  • FIG. 6 is a diagram showing a configuration of a prime mover system 1a according to the second embodiment of the present invention.
  • the prime mover system 1a includes a supercharger-equipped prime mover 2 having a structure similar to that shown in FIG. 1, and a waste heat recovery device 6a having a structure different from that of the waste heat recovery device 6 shown in FIG.
  • a regenerator 66 is provided in addition to the structure of the waste heat recovery apparatus 6 shown in FIG.
  • the other structure of the waste heat recovery apparatus 6a is almost the same as that of the waste heat recovery apparatus 6 shown in FIG. 1, and the same reference numerals are given in the following description.
  • the regenerator 66 is disposed between the expander 63 and the condenser 64 and between the pump 65 and the exhaust heat exchanger 622 on the pipe 61.
  • a liquid working fluid (that is, R4310mee) is pressurized by the pump 65 and sent to the regenerator 66.
  • the pressure of the working fluid delivered from the pump 65 is lower than the critical pressure of the working fluid.
  • the regenerator 66 the liquid working fluid led from the pump 65 to the exhaust heat exchanger 622 is heated by the gaseous working fluid led from the expander 63 to the condenser 64.
  • the liquid working fluid heated in the regenerator 66 is guided to the exhaust heat exchanger 622, and the exhaust gas from the turbine 41 of the supercharger 4 flowing through the exhaust path 32 (that is, the prime mover 3).
  • the exhaust gas is heated using a heat source.
  • the liquid working fluid from the regenerator 66 is heated by the preheater 623 of the exhaust heat exchanger 622 using the exhaust as a heat source, and further heated by the evaporator 624 using the exhaust as a heat source and vaporized.
  • the working fluid vaporized in the exhaust heat exchanger 622 is in a saturated steam state, for example, and is guided to the expander 63.
  • the expander 63 expands the working fluid heated and vaporized by the exhaust heat exchanger 622 and recovers mechanical energy. And in the generator 8 connected to the expander 63, electric power generation is performed using the mechanical energy.
  • the gaseous working fluid delivered from the expander 63 is cooled by exchanging heat with the liquid working fluid guided from the pump 65 to the exhaust heat exchanger 622 in the regenerator 66. .
  • the working fluid cooled by the regenerator 66 is guided to the condenser 64 where it is condensed and liquefied.
  • the working fluid liquefied by the condenser 64 is pressurized by the pump 65 and sent to the regenerator 66, passes through the regenerator 66, and is sent to the exhaust heat exchanger 622.
  • the working fluid led from the pump 65 to the exhaust heat exchanger 622 is heated by the working fluid led from the expander 63 to the condenser 64.
  • the exhaust heat exchanger 622 energy required for heating the unit amount of working fluid to a predetermined state can be reduced.
  • the flow rate of the working fluid in the exhaust heat exchanger 622 can be increased, and the flow rate of the working fluid guided from the exhaust heat exchanger 622 to the expander 63 can also be increased.
  • the efficiency of waste heat recovery by the waste heat recovery device 6a can be improved.
  • the working fluid led from the expander 63 to the condenser 64 is cooled by the liquid working fluid led from the pump 65 to the exhaust heat exchanger 622. For this reason, in the condenser 64, the energy required to liquefy a unit amount of working fluid can be reduced. Thereby, the efficiency of waste heat recovery by the waste heat recovery apparatus 6a can be further improved.
  • the saturated vapor line of R4310mee which is the working fluid of the waste heat recovery apparatus 6a
  • the saturated vapor line of R4310mee has a positive gradient on the TS diagram (see FIG. 2).
  • the saturated steam of the working fluid is expanded in the expander 63
  • the expanded working fluid is dry steam. Therefore, in the regenerator 66, the working fluid condensed by the condenser 64 can be heated by sensible heat from the temperature of the dry steam to the condensation temperature. As a result, the efficiency of waste heat recovery in the ORC using the regenerator 66 can be further improved.
  • FIG. 7 is a diagram showing the relationship between the expander inlet temperature and the recovery power in the waste heat recovery apparatus 6a.
  • the horizontal axis in FIG. 7 indicates the expander inlet temperature, and the vertical axis indicates the recovery power ratio.
  • the recovery power ratio is also shown for the waste heat recovery device of the second comparative example using R245fa as the working fluid.
  • the waste heat recovery apparatus of the second comparative example has the same configuration as the waste heat recovery apparatus 6a shown in FIG. 6, and uses R245fa as a working fluid instead of R4310mee.
  • the recovery power ratio of the waste heat recovery apparatus 6a is indicated by a solid line 91
  • the recovery power ratio of the waste heat recovery apparatus of the second comparative example is indicated by a broken line 92.
  • the recovery power ratios of the waste heat recovery device 6a and the waste heat recovery device of the second comparative example are the recovery power at each expander inlet temperature, and the waste heat recovery when the expander inlet temperature is about 260 ° C. It is obtained by dividing by the recovery power of the device 6a.
  • the recovery power of the waste heat recovery apparatus 6a is obtained by calculation assuming that the evaporation temperature and the evaporation pressure of R4310mee, which is a working fluid, are about 180 ° C. and about 2.1 MPa, respectively.
  • the recovery power of the waste heat recovery apparatus of the second comparative example is obtained by calculation assuming that the evaporation temperature and the evaporation pressure of R245fa as the working fluid are about 140 ° C. and about 2.8 MPa, respectively.
  • the recovery power of the waste heat recovery device 6a shown in FIG. 6 is larger than the recovery power of the waste heat recovery device of the second comparative example.
  • the recovery power of the waste heat recovery device 6a is the second comparison even when the expander inlet temperature is lower than 210 ° C and when the expander inlet temperature is higher than 330 ° C. It is larger than the recovery power of the waste heat recovery device in the example.
  • the waste heat of the prime mover 3 can be recovered efficiently compared to the waste heat recovery device of the second comparative example.
  • R245fa that is a working fluid is thermally decomposed in a relatively short time in a high temperature range (for example, a temperature range higher than 300 ° C.).
  • a high temperature range for example, a temperature range higher than 300 ° C.
  • the working fluid R4310mee has thermal stability even at about 500 ° C. as described above, so the waste heat of the prime mover 3 that is a relatively high-temperature heat source is removed. It can be recovered efficiently and stably.
  • FIG. 8 is a diagram showing a configuration of a prime mover system 1b according to the third embodiment of the present invention.
  • the prime mover system 1b includes a supercharger-equipped prime mover 2 having a structure similar to that shown in FIG. 1, and a waste heat recovery device 6b having a structure different from that of the waste heat recovery device 6 shown in FIG.
  • an exhaust heat exchanger 622a having a structure different from that of the exhaust heat exchanger 622 shown in FIG. 1 is provided.
  • the evaporator 624 see FIG. 1) for vaporizing R4310mee, which is a working fluid, is omitted.
  • a compressed air heat exchanger 621 is disposed on the pipe 61 between the pump 65 and the exhaust heat exchanger 622a.
  • the other structure of the waste heat recovery apparatus 6b is almost the same as that of the waste heat recovery apparatus 6 shown in FIG. 1, and the same reference numerals are given in the following description.
  • the compressed air heat exchanger 621 is provided on the air supply path 31.
  • the liquid working fluid sent from the pump 65 is preliminarily heated using the supply air from the compressor 42 flowing through the supply air passage 31 as a heat source.
  • the working fluid is heated using heat generated to cool the compressed air (that is, waste heat of the supercharger-equipped prime mover 2 included in the supply air) as a heat source.
  • the temperature of the supply air flowing into the compressed air heat exchanger 621 is about 130 to 210 ° C., for example.
  • the temperature of the supply air varies relatively greatly depending on the output of the prime mover 3.
  • FIG. 9 is a TS diagram of the waste heat recovery apparatus 6b.
  • the horizontal axis of FIG. 9 shows specific entropy, and the vertical axis shows temperature.
  • a solid line 906 in FIG. 9 indicates the ORC in the waste heat recovery apparatus 6b.
  • broken lines 902 and 903 in FIG. 9 are a saturated liquid line and a saturated vapor line of R4310mee, which is a working fluid of the waste heat recovery apparatus 6b, respectively.
  • the liquid working fluid (that is, R4310mee) is pressurized by the pump 65 and sent to the compressed air heat exchanger 621 in the waste heat recovery apparatus 6b shown in FIG.
  • the pressure of the working fluid sent out by the pump 65 is higher than that of the waste heat recovery device 6 shown in FIG. 1 and higher than the critical pressure of the working fluid.
  • the critical pressure of R4310mee is about 2.2 MPa as described above.
  • the liquid working fluid is preliminarily heated using the air supplied from the compressor 42 flowing through the air supply passage 31 as a heat source.
  • the liquid working fluid sent from the compressed air heat exchanger 621 is guided to the exhaust heat exchanger 622a through the pipe 61.
  • the liquid working fluid sent from the compressed air heat exchanger 621 heats the exhaust from the turbine 41 of the supercharger 4 flowing through the exhaust passage 32 (that is, the exhaust of the prime mover 3) as a heat source. Is done.
  • the working fluid is heated to a temperature higher than the critical temperature of the working fluid.
  • the critical temperature means the temperature at the critical point of the working fluid.
  • the critical temperature of R4310mee is about 181 ° C.
  • the working fluid sent from the exhaust heat exchanger 622a and guided to the expander 63 is in a supercritical state where the pressure and temperature are higher than the critical pressure and critical temperature.
  • the liquid working fluid delivered from the compressed air heat exchanger 621 is heated by the exhaust heat exchanger 622a to be in a supercritical state corresponding to the point 907 in FIG.
  • the expander 63 expands the supercritical working fluid and recovers mechanical energy. And in the generator 8 connected to the expander 63, electric power generation is performed using the mechanical energy. Since the critical temperature and critical pressure of R4310mee are lower than the temperature and pressure of water vapor in a normal steam boiler, the expansion machine 63 can easily realize the expansion of R4310mee in a supercritical state. In the expander 63, the working fluid in a supercritical state corresponding to the point 907 in FIG. 9 expands, and is sent out in a superheated steam state corresponding to the point 908 in FIG.
  • the working fluid in the superheated vapor state sent from the expander 63 is guided to the condenser 64, where it is condensed and liquefied.
  • the working fluid liquefied by the condenser 64 is pressurized to a pressure higher than the critical pressure by the pump 65, sent to the compressed air heat exchanger 621, and passes through the compressed air heat exchanger 621. Then, it is sent to the exhaust heat exchanger 622.
  • FIG. 10 is a diagram showing a comparison between the recovery power in the waste heat recovery apparatus 6b shown in FIG. 8 and the recovery power in the waste heat recovery apparatus 6 shown in FIG.
  • the waste heat recovery apparatuses 6 and 6b are common in that they do not have the regenerator 66 (see FIG. 6), and are different from each other in that the waste heat recovery apparatus 6b has a compressed air heat exchanger 621. Further, they differ from each other in that the waste heat recovery device 6b uses a supercritical working fluid and the waste heat recovery device 6 does not use a supercritical working fluid.
  • the horizontal axis of FIG. 10 shows the evaporation temperature of the working fluid (that is, R4310mee) in the exhaust heat exchanger 622 of the waste heat recovery apparatus 6 shown in FIG.
  • the vertical axis in FIG. 10 indicates the recovery power ratio of the waste heat recovery apparatuses 6 and 6b.
  • the recovery power ratio of the waste heat recovery apparatuses 6 and 6b is obtained by dividing the recovery power of the waste heat recovery apparatuses 6 and 6b by the recovery power of the waste heat recovery apparatus 6 when the evaporation temperature is 130 ° C.
  • the recovery power ratio in the waste heat recovery apparatus 6 at the evaporation temperatures of 130 ° C., 140 ° C., 150 ° C., 160 ° C. and 170 ° C. is indicated by hollow circles. Further, in the waste heat recovery apparatus 6b shown in FIG. 8, since the working fluid is not vaporized in the exhaust heat exchanger 622a, the recovery power in the waste heat recovery apparatus 6b is irrelevant to the value on the horizontal axis in FIG. In FIG. 10, the recovery power in the waste heat recovery device 6 b is indicated by a solid line 93.
  • the recovery power (solid line 93) in the waste heat recovery apparatus 6b is such that the temperature of the supply air from the compressor 42 is 200 ° C., the temperature of the exhaust from the turbine 41 is 415 ° C., and the exhaust heat exchanger 622a to the expander 63.
  • the expander inlet temperature and expander inlet pressure, which are the temperature and pressure of the inflowing working fluid, are set to 350 ° C. and 3.0 MPa, respectively, and the condensing temperature of the working fluid in the condenser 64 is determined to be 38 ° C. by calculation.
  • the recovery power (circles) in the waste heat recovery apparatus 6 is the same as the above in the temperature of the supply air from the compressor 42, the temperature of the exhaust from the turbine 41, and the condensation temperature of the working fluid in the condenser 64, respectively. It is calculated by assuming that the working fluid vaporized at each evaporation temperature is 200 ° C., 415 ° C. and 38 ° C. and heated to 350 ° C. in the exhaust heat exchanger 622 and then supplied to the expander 63.
  • the evaporation pressure of the working fluid at the evaporation temperatures of 130 ° C., 140 ° C., 150 ° C., 160 ° C. and 170 ° C. is about 0.8 MPa, about 1.0 MPa, about 1.3 MPa, about 1.5 MPa and about 1.9 MPa.
  • the recovery power in the waste heat recovery device 6b (see FIG. 8) using the supercritical working fluid is the waste heat recovery device 6 (see FIG. 1) that does not use the supercritical working fluid. Is greater than the recovery power at, regardless of the evaporation temperature in the exhaust heat exchanger 622 of the waste heat recovery device 6. That is, in the waste heat recovery device 6b, the waste heat recovery efficiency can be improved as compared with the waste heat recovery device 6.
  • the waste heat recovery device 6 Since the waste heat recovery device 6 does not use a supercritical working fluid, it is necessary to apply heat for latent heat in heating the working fluid. However, the waste heat recovery device 6b uses a supercritical working fluid. By doing so, it becomes unnecessary to apply heat for latent heat. Whether or not the application of heat for the latent heat is necessary contributes to the difference in the recovery power described above.
  • the expander inlet temperature of the waste heat recovery device 6 b is equal to the expander inlet temperature of the waste heat recovery device 6, but the expander inlet pressure of the waste heat recovery device 6 b is the expander of the waste heat recovery device 6. Greater than inlet pressure. For this reason, the heat drop in the expander 63 of the waste heat recovery apparatus 6b is larger than the heat drop in the expander 63 of the waste heat recovery apparatus 6. The difference in the heat drop is also a cause of the difference in the recovery power described above.
  • the exhaust heat of the prime mover 3 can be efficiently recovered by heating the working fluid by the exhaust of the relatively high temperature prime mover 3 in the exhaust heat exchanger 622a. Further, in the compressed air heat exchanger 621, waste heat of the prime mover 3 can be recovered more efficiently by preliminarily heating the working fluid using the supply air as a heat source and then sending it to the exhaust heat exchanger 622a. .
  • the temperature of the exhaust gas flowing into the exhaust heat exchanger 622a is, for example, about 420 ° C.
  • the temperature of the supply air flowing into the compressed air heat exchanger 621 is, for example, about 130. ⁇ 210 ° C.
  • the waste heat of the relatively low temperature supply air is used for preliminary heating of the working fluid in the compressed air heat exchanger 621, and the waste heat of the relatively high temperature exhaust is exhausted. This is used for heating the working fluid in the heat exchanger 622a.
  • the installation area of the device can be reduced and the operation management of the device can be simplified.
  • FIG. 11 is a diagram showing the relationship between the output of the prime mover 3, the exhaust gas temperature, and the supply air temperature.
  • the horizontal axis of FIG. 11 indicates the output ratio of the prime mover 3 (that is, the ratio of output to the maximum output), and the vertical axis indicates the exhaust temperature and the supply air temperature in a dimensionless manner.
  • the non-dimensionalization of the exhaust temperature and the supply air temperature is performed by dividing the exhaust temperature and the supply air temperature by the exhaust temperature when the output ratio is 100%.
  • the exhaust temperature indicated by the solid square is approximately constant regardless of the output ratio of the prime mover 3, but the supply air temperature indicated by the hollow square decreases the output ratio of the prime mover 3. It decreases gradually as you go.
  • FIG. 12 is a diagram showing the relationship between the temperature of the supply air from the compressor 42 and the recovery power in the waste heat recovery apparatus 6b.
  • the horizontal axis in FIG. 12 indicates the supply air temperature, and the vertical axis indicates the recovery power ratio.
  • the recovery power ratio is obtained by dividing the recovery power in the waste heat recovery device 6b by the recovery power in the waste heat recovery device 6 when the evaporation temperature is 130 ° C., as in FIG.
  • the recovery power in the waste heat recovery device 6b is the maximum recovery power in the waste heat recovery device 6 when the supply air temperature is 200 ° C. (that is, evaporation in FIG. 10) even when the supply air temperature is 130 ° C. This is almost equal to the recovery power of the waste heat recovery device 6 when the temperature is about 160 ° C. Therefore, the recovery power in the waste heat recovery device 6b when the supply air temperature is 130 ° C. is naturally larger than the maximum recovery power in the waste heat recovery device 6 when the supply air temperature is 130 ° C.
  • the recovery power in the waste heat recovery apparatus 6b using the supercritical working fluid is the waste heat recovery apparatus 6 that does not use the supercritical working fluid regardless of the temperature of the supply air from the compressor 42. Greater than recovery power. That is, in the waste heat recovery device 6b, even when the supply air temperature fluctuates due to the output fluctuation of the prime mover 3, the waste associated with the prime mover 3 is maintained while maintaining high recovery efficiency corresponding to the fluctuation of the supply air temperature. Heat can be recovered.
  • FIG. 13 is a diagram showing the relationship between the expander inlet temperature and the recovery power in the waste heat recovery apparatus 6b shown in FIG.
  • the horizontal axis in FIG. 13 indicates the expander inlet temperature, and the vertical axis indicates the recovery power ratio.
  • the recovery power ratio is also shown for the waste heat recovery apparatus of the third comparative example.
  • the waste heat recovery apparatus of the third comparative example has the same configuration as the waste heat recovery apparatus 6b shown in FIG. 8, and uses R245fa as the working fluid instead of R4310mee.
  • the working fluid (R245fa) heated to the supercritical state in the exhaust heat exchanger is supplied to the expander.
  • the critical temperature and critical pressure of R245fa are about 150 ° C. and about 3.7 MPa, respectively.
  • the recovery power ratio of the waste heat recovery device 6 b is indicated by a solid line 94
  • the recovery power ratio of the waste heat recovery device of the third comparative example is indicated by a broken line 95.
  • the recovery power ratios of the waste heat recovery device 6b and the waste heat recovery device of the third comparative example are the recovery power at each expander inlet temperature, and the waste heat recovery when the expander inlet temperature is about 250 ° C. It is obtained by dividing by the recovery power of the device 6b.
  • the recovery power of the waste heat recovery device 6b is obtained by calculation with the expander inlet pressure of R4310mee, which is a working fluid, being about 3.0 MPa.
  • the recovery power of the waste heat recovery apparatus of the third comparative example can be obtained by calculation with the expander inlet pressure of R245fa, which is the working fluid, being about 4.0 MPa.
  • the recovery power of the waste heat recovery device 6b shown in FIG. 8 is larger than the recovery power of the waste heat recovery device of the third comparative example.
  • the recovery power of the waste heat recovery device 6b is the third comparison even when the expander inlet temperature is lower than 250 ° C. and when the expander inlet temperature is higher than 350 ° C. It is larger than the recovery power of the waste heat recovery device in the example.
  • the waste heat recovery device 6b can efficiently recover the waste heat of the prime mover 3.
  • the waste heat recovery apparatus of the third comparative example actually, R245fa as the working fluid is thermally decomposed in a relatively short time in a high temperature range (for example, a temperature range higher than 300 ° C.).
  • a high temperature range for example, a temperature range higher than 300 ° C.
  • the working fluid R4310mee has thermal stability even at about 500 ° C. as described above, so the waste heat of the prime mover 3 that is a relatively high-temperature heat source is removed. It can be recovered efficiently and stably.
  • FIG. 14 is a diagram showing a configuration of a prime mover system 1c according to the fourth embodiment of the present invention.
  • the prime mover system 1c includes a supercharger-equipped prime mover 2 having a structure similar to that shown in FIG. 8, and a waste heat recovery device 6c having a structure different from that of the waste heat recovery device 6b shown in FIG.
  • a regenerator 66 is provided in addition to the structure of the waste heat recovery apparatus 6b shown in FIG.
  • the other structure of the waste heat recovery device 6c is substantially the same as that of the waste heat recovery device 6b shown in FIG. 8, and the same reference numerals are given in the following description.
  • the regenerator 66 is disposed on the pipe 61 between the expander 63 and the condenser 64 and between the compressed air heat exchanger 621 and the exhaust heat exchanger 622a.
  • a liquid working fluid (that is, R4310mee) is pressurized by the pump 65 and sent to the compressed air heat exchanger 621.
  • the pressure of the working fluid delivered from the pump 65 is higher than the critical pressure of the working fluid, like the waste heat recovery device 6b shown in FIG.
  • the liquid working fluid is preliminarily heated using the air supplied from the compressor 42 flowing through the air supply passage 31 as a heat source.
  • the liquid working fluid sent from the compressed air heat exchanger 621 is guided to the exhaust heat exchanger 622a through the regenerator 66 by the pipe 61.
  • the regenerator 66 the liquid working fluid led from the compressed air heat exchanger 621 to the exhaust heat exchanger 622a is heated by the gaseous working fluid led from the expander 63 to the condenser 64.
  • the liquid working fluid heated in the regenerator 66 is guided to the exhaust heat exchanger 622a, and the exhaust gas from the turbine 41 of the supercharger 4 flowing through the exhaust path 32 (that is, the prime mover 3) in the exhaust heat exchanger 622a.
  • the exhaust gas is heated using a heat source.
  • the working fluid is heated to a temperature higher than the critical temperature of the working fluid and becomes a supercritical state.
  • the expander 63 expands the working fluid in a supercritical state and recovers mechanical energy.
  • electric power generation is performed using the mechanical energy.
  • the supercritical working fluid expands and is delivered in a superheated steam state.
  • the superheated steam working fluid sent from the expander 63 exchanges heat with the liquid working fluid led from the compressed air heat exchanger 621 to the exhaust heat exchanger 622a in the regenerator 66 as described above. It is cooled by.
  • the working fluid cooled by the regenerator 66 is guided to the condenser 64 where it is condensed and liquefied.
  • the working fluid liquefied by the condenser 64 is pressurized to a pressure higher than the critical pressure by the pump 65, sent to the compressed air heat exchanger 621, and passes through the compressed air heat exchanger 621. Then, it is sent to the exhaust heat exchanger 622a.
  • the operation fluid that is guided from the expander 63 to the condenser 64 is guided from the compressed air heat exchanger 621 to the exhaust heat exchanger 622a.
  • the fluid is heated.
  • energy required for heating the unit amount of working fluid to a predetermined supercritical state can be reduced.
  • the flow rate of the working fluid in the exhaust heat exchanger 622a can be increased, and the flow rate of the working fluid guided from the exhaust heat exchanger 622a to the expander 63 can also be increased.
  • the efficiency of waste heat recovery by the waste heat recovery device 6c can be improved.
  • the working fluid led from the expander 63 to the condenser 64 is cooled by the liquid working fluid led from the compressed air heat exchanger 621 to the exhaust heat exchanger 622a. For this reason, in the condenser 64, the energy required to liquefy a unit amount of working fluid can be reduced. Thereby, the efficiency of waste heat recovery by the waste heat recovery device 6c can be further improved.
  • the supercritical working fluid supplied to the expander 63 expands to become a relatively high-temperature superheated steam.
  • the turbine efficiency of the expander 63 is about 65% and the expander inlet temperature and the expander inlet pressure of the working fluid are about 350 ° C. and about 3.0 MPa, respectively
  • the expander 63 to the regenerator 66 The temperature of the superheated steam working fluid supplied to is about 290-300 ° C.
  • the working fluid condensed by the condenser 64 can be heated by sensible heat from the temperature of the relatively high superheated steam to the condensation temperature.
  • the efficiency of waste heat recovery in the ORC using the working fluid in the supercritical state and also using the regenerator 66 can be further improved.
  • the working fluid sent from the compressed air heat exchanger 621 can be heated by the working fluid in a superheated steam state having a relatively high temperature. Therefore, the output of the prime mover 3 is relatively small, and the compressed air is compressed. Even when the supply air temperature in the heat exchanger 621 is relatively low, the working fluid can be sufficiently heated in the regenerator 66 and supplied to the exhaust heat exchanger 622a. Therefore, in the waste heat recovery device 6c, even when the supply air temperature fluctuates due to the output fluctuation of the prime mover 3, the waste associated with the prime mover 3 is maintained while maintaining high recovery efficiency corresponding to the fluctuation of the supply air temperature. Heat can be recovered.
  • FIG. 15 is a diagram showing a comparison between the recovery power in the waste heat recovery apparatus 6c shown in FIG. 14 and the recovery power in the waste heat recovery apparatus 6b shown in FIG.
  • the waste heat recovery devices 6b and 6c are common in that they use a supercritical working fluid (that is, R4310mee).
  • the waste heat recovery device 6c is different from each other in that a regenerator 66 is provided, and the waste heat recovery device 6b is not provided with a regenerator.
  • the horizontal axis of FIG. 15 indicates the supply air temperature in the waste heat recovery apparatuses 6b and 6c, and the vertical axis indicates the recovery power ratio of the waste heat recovery apparatuses 6b and 6c.
  • the recovery power ratio of the waste heat recovery devices 6b and 6c is obtained by dividing the recovery power in the waste heat recovery devices 6b and 6c by the recovery power in the waste heat recovery device 6b when the supply air temperature is 130 ° C.
  • the recovery power ratios in the waste heat recovery apparatuses 6b and 6c when the supply air temperature is 130 ° C., 150 ° C., 180 ° C., and 200 ° C. are indicated by hollow circles and solid circles, respectively.
  • the recovery power (solid circles) in the waste heat recovery device 6c is the temperature and pressure of the working fluid flowing from the exhaust heat exchanger 622a to the expander 63 when the temperature of the exhaust from the turbine 41 is 415 ° C.
  • the expansion machine inlet temperature and the expansion machine inlet pressure are set to 350 ° C. and 3.0 MPa
  • the condensation temperature of the working fluid in the condenser 64 is set to 38 ° C.
  • the temperature of the working fluid flowing into the exhaust heat exchanger 622a is calculated to be 200 ° C. Is required.
  • the recovery power of the waste heat recovery device 6c is heated to 200 ° C. regardless of the supply air temperature when the working fluid sent from the condenser 64 passes through the compressed air heat exchanger 621 and the regenerator 66. Is required.
  • the recovery power (hollow circle) in the waste heat recovery device 6b is the exhaust temperature from the turbine 41, the expander inlet temperature, the expander inlet pressure, and the condensation temperature of the working fluid in the condenser 64, respectively. Similarly, 415 ° C., 350 ° C., 3.0 MPa, and 38 ° C. are obtained by calculation.
  • the temperature of the working fluid flowing into the exhaust heat exchanger 622a that is, the temperature of the working fluid heated by the compressed air heat exchanger 621 depends on the supply air temperature. Be changed. Specifically, when the supply air temperature is 130 ° C., 150 ° C., 180 ° C. and 200 ° C., the temperature of the working fluid flowing into the exhaust heat exchanger 622a is 100 ° C., 120 ° C., 150 ° C. and 160 ° C., respectively. is there.
  • the recovery power in the waste heat recovery device 6c (see FIG. 14) using the working fluid in the supercritical state and including the regenerator 66 is used for the recovery power using the working fluid in the supercritical state. It is larger than the recovery power in the waste heat recovery apparatus 6b (see FIG. 8) that does not have, regardless of the supply air temperature. That is, in the waste heat recovery device 6c, by providing the regenerator 66, the waste heat recovery efficiency can be improved as compared with the waste heat recovery device 6b as described above.
  • waste heat recovery devices 6, 6a to 6c can be variously modified.
  • FIG. 16 is a TS diagram of the waste heat recovery apparatus 6 provided with a superheater.
  • the working fluid vaporized in the evaporator 624 is heated in the superheater using the exhaust from the turbine 41 as a heat source to become superheated steam.
  • a point 909 in FIG. 16 corresponds to the working fluid in the superheated steam state.
  • the working fluid in the superheated steam state is expanded by the expander 63. Thereby, the recovery efficiency of the waste heat in the waste heat recovery apparatuses 6 and 6a can be improved.
  • a compressed air heat exchanger 621 using heat supplied from the compressor 42 as a heat source may be provided.
  • the compressed air heat exchanger 621 is disposed between the pump 65 and the exhaust heat exchanger 622 on the pipe 61.
  • the compressed air heat exchanger 621 using the supply air from the compressor 42 as a heat source is omitted, and only the waste heat of the exhaust is recovered by the exhaust heat exchanger 622a as waste heat from the prime mover 3. May be.
  • another heat exchanger that heats the R4310mee, which is a working fluid, using the jacket cooling water of the prime mover 3 as a heat source may be further provided.
  • a heat exchanger using jacket cooling water as a heat source is disposed on the pipe 61 between the pump 65 and the exhaust heat exchanger 622.
  • the heat exchanger using the jacket cooling water as a heat source is disposed on the pipe 61 between the pump 65 and the compressed air heat exchanger 621.
  • a heat exchanger using the jacket cooling water as a heat source may be provided.
  • the prime mover 3 may be, for example, a two-cycle gas engine.
  • the compressed air that is the intake air pressurized by the compressor 42 is called “scavenging”, and the air supply path 31 is called a scavenging path.
  • the prime mover 3 may be an internal combustion engine other than a gas engine, or may be a prime mover other than the internal combustion engine.
  • the waste heat recovery devices 6, 6a to 6c can be used in various facilities other than the prime mover system.
  • the waste heat recovery devices 6, 6a to 6c include R4310mee, which is a working fluid using the waste heat of various devices as a heat source.
  • a heat exchanger may be provided that heats. Even in this case, the waste heat recovery devices 6, 6a to 6c can recover the waste heat efficiently and stably from a relatively high temperature heat source, as described above.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention porte sur un dispositif de récupération de chaleur perdue (6), lequel dispositif comporte une conduite (61), un échangeur de chaleur à air comprimé (621), un échangeur de chaleur à air d'échappement (622), une machine de détente (63), un condenseur (64), et une pompe (65). Un fluide de travail s'écoulant à travers la conduite (61) est du R4310mee. Le fluide de travail est chauffé à l'aide d'air d'alimentation vers un moteur (3), constituant une source de chaleur dans l'échangeur de chaleur à air comprimé (621), et chauffé à l'aide d'air d'échappement venant du moteur (3), constituant une source de chaleur, et gazéifié dans l'échangeur de chaleur à air d'échappement (622). La machine de détente (63) détend le fluide de travail gazeux et récupère une énergie mécanique. Le fluide de travail détendu est condensé et liquéfié dans le condenseur (64), et délivré à l'échangeur de chaleur à air comprimé (621) par la pompe (65). Dans le dispositif de récupération de chaleur perdue (6), le R4310mee, qui est le fluide de travail, a une stabilité thermique même à approximativement 500° C. Par conséquent, une chaleur perdue peut être récupérée efficacement et de façon stable à partir de l'air d'échappement, qui est une source de chaleur à température relativement élevée venant du moteur (3).
PCT/JP2014/069827 2013-08-07 2014-07-28 Dispositif de récupération de chaleur perdue WO2015019886A1 (fr)

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JP2018168758A (ja) * 2017-03-30 2018-11-01 日野自動車株式会社 廃熱回収装置

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EP3216989A1 (fr) * 2016-03-11 2017-09-13 NEM Energy B.V. Centrale electrique à cycle combiné
KR102016415B1 (ko) * 2018-03-09 2019-08-30 삼성중공업 주식회사 압축 공기 생성 장치
JP7290520B2 (ja) * 2019-09-04 2023-06-13 メタウォーター株式会社 Ｏｒｃ発電システム

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JP2008506819A (ja) * 2004-07-16 2008-03-06 ハネウェル・インターナショナル・インコーポレーテッド ランキンサイクルシステムを用いて燃料電池からの廃熱を熱エネルギー変換するための作動流体
JP2011231636A (ja) * 2010-04-26 2011-11-17 Mitsubishi Heavy Ind Ltd 排熱回収発電装置およびこれを備えた船舶
JP2012026441A (ja) * 2010-07-23 2012-02-09 General Electric Co <Ge> ハイブリッド発電システム及びその方法
WO2013108867A1 (fr) * 2012-01-20 2013-07-25 日立造船株式会社 Appareil de récupération de la chaleur perdue et système moteur primaire

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JP2008506819A (ja) * 2004-07-16 2008-03-06 ハネウェル・インターナショナル・インコーポレーテッド ランキンサイクルシステムを用いて燃料電池からの廃熱を熱エネルギー変換するための作動流体
JP2011231636A (ja) * 2010-04-26 2011-11-17 Mitsubishi Heavy Ind Ltd 排熱回収発電装置およびこれを備えた船舶
JP2012026441A (ja) * 2010-07-23 2012-02-09 General Electric Co <Ge> ハイブリッド発電システム及びその方法
WO2013108867A1 (fr) * 2012-01-20 2013-07-25 日立造船株式会社 Appareil de récupération de la chaleur perdue et système moteur primaire

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Publication number Priority date Publication date Assignee Title
JP2018168758A (ja) * 2017-03-30 2018-11-01 日野自動車株式会社 廃熱回収装置

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