WO2018200856A1 - Procédés, systèmes et appareil de production d'énergie, de réfrigération et de récupération de chaleur perdue combinées - Google Patents

Procédés, systèmes et appareil de production d'énergie, de réfrigération et de récupération de chaleur perdue combinées Download PDF

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Publication number
WO2018200856A1
WO2018200856A1 PCT/US2018/029627 US2018029627W WO2018200856A1 WO 2018200856 A1 WO2018200856 A1 WO 2018200856A1 US 2018029627 W US2018029627 W US 2018029627W WO 2018200856 A1 WO2018200856 A1 WO 2018200856A1
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Prior art keywords
power generator
rankine cycle
cycle power
vcr
working fluid
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PCT/US2018/029627
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English (en)
Inventor
Donald Williams
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M-Trigen, Inc.
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Publication of WO2018200856A1 publication Critical patent/WO2018200856A1/fr

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Classifications

    • 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
    • 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
    • F01K23/10—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 with exhaust fluid of one cycle heating the fluid in another cycle
    • 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
    • F01K25/10—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 the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • 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
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/14—Combined heat and power generation [CHP]
    • 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 disclosure relates generally to Rankine cycle power generators and vapor compression cooling systems, and in particular to organic Rankine cycles using high molecular mass refrigerants with low boiling points suited for low-grade heat applications, and to Rankine cycles thermally coupled with both a vapor compression refrigeration cycle (VRC) and the exhaust of a combined heating and power (CHP) system or combined cooling, heating and power (CCHP) system.
  • VRC vapor compression refrigeration cycle
  • CHP heating and power
  • CCHP combined cooling, heating and power
  • the present disclosure is directed to Rankine cycle power generators and vapor compression cooling systems. More particularly, the present disclosure is directed to organic Rankine cycles that use high molecular mass refrigerants with low boiling points suited for low-grade heat applications.
  • the present disclosure relates systems and methods to increase the fuel efficiency of a CHP or CCHP system containing a fossil fueled engine, VCR cycle and a waste heat recovery subsystem.
  • the waste heat recovery subsystem includes an organic Rankine cycle that converts engine combustion and VCR waste heats to mechanical and/or electrical energy.
  • the methods and systems disclosed herein use both the engine combustion and vapor compression waste heats of a CHP or CCHP system to power a low temperature organic Rankin power converter in a ORC-VCR system.
  • the methods and systems disclosed herein use the waste heat discharged from the vapor compression system to increase Rankin efficiency.
  • the methods and systems disclosed herein are characterized in that they allow for the organic Rankine cycle to be readily integrated or retrofitted with existing vapor compression systems.
  • the method includes operatively coupling an organic Rankine cycle power generator to a CHP or a CCHP system, including an engine and a vapor compression refrigeration (VCR) cycle.
  • the method includes transferring waste heat from the engine to a working fluid of the Rankine cycle power generator and transferring waste heat from a working fluid of the VCR cycle to the working fluid of the Rankine cycle power generator.
  • operatively coupling the organic Rankine cycle power generator to the CCHP system includes retrofitting an existing CCHP system to integrate the organic Rankine cycle power generator therein.
  • the thermal efficiency of the organic Rankine cycle power generator may be greater than 1 1%, greater than 12%, or greater than 13%.
  • One embodiment disclosed herein relates to a method to increase the efficiency of a CCHP system in which an organic Rankine cycle generator is employed to utilize CCHP and cooling system waste heat.
  • the CCHP engine waste heat is transferred to the Rankine cycle via a heat exchanger, thereby allowing sensible heat transfer from the engine to the working fluid of the Rankine cycle.
  • the heat transfer may occur via either convection of combustion exhaust gas internal energy and/or conduction of heat through engine support hardware via a first heat exchanger device.
  • the cooling subsystem of the CCHP system is a vapor compression refrigeration (VCR) cycle.
  • VCR vapor compression refrigeration
  • Certain embodiments of the present disclosure relate to a system including an organic Rankine cycle power generator operatively coupled to an engine and a VCR cycle of a CCHP system.
  • Some embodiments of the present disclosure include a method of providing cooling, heating, and/or power to a local environment.
  • the method includes generating mechanical energy using an engine.
  • the engine produces waste heat as thermal energy.
  • the method includes providing air conditioning to a local environment using a vapor compression refrigeration (VCR) cycle.
  • VCR vapor compression refrigeration
  • the method includes transferring at least a portion of the thermal energy of waste heat produced by the engine and the VCR cycle into a working fluid of a Rankine cycle power generator and converting the thermal energy within the Rankine cycle power generator into mechanical energy, electrical energy, or combinations thereof.
  • FIG. 1 is a diagram of combined organic Rankine and vapor compression refrigeration (ORC-VCR) system
  • FIG. 2 is a mass flow and energy analysis of an ORC-VCR system using R-134a as the Rankine cycle refrigerant
  • FIG. 3 is a mass flow and energy analysis of an ORC-VCR system using R-245fa as the Rankine cycle refrigerant
  • FIG. 4 is a pressure-enthalpy (P-H) chart of the ORC-VCR system of FIG. 2;
  • FIG. 5 is a pressure-enthalpy (P-H) chart of the ORC-VCR system of FIG. 3;
  • FIG. 6 is a process flow diagram of a Rankine cycle with DR-2 as the Rankine cycle refrigerant
  • FIG. 7 is a process flow diagram of an optimized Rankine cycle with DR-2 as the Rankine cycle refrigerant
  • FIG. 8 is a Mollier Diagram of the DR-2 Rankine Cycle
  • FIG. 9 is a Mollier Diagram of an Optimized DR-2 Rankine Cycle.
  • FIG. 10 depicts a simplified schematic of a system in accordance with certain embodiments of the present disclosure.
  • the present disclosure relates to systems, apparatus, and methods for transferring waste heat energy from both an engine and a VCR cycle of a CCHP system to an organic Rankine cycle generator.
  • the organic Rankine cycle generator may then convert the energy of the transferred waste heat into another form of energy, such as mechanical energy, electrical energy, or combinations thereof.
  • the energy formed by the organic Rankine cycle generator may then be used to power other apparatus or systems, for example.
  • FIG. 1 is a diagram a system, in accordance with certain embodiments of the present disclosure.
  • System 1000 is a combined organic Rankine and vapor compression refrigeration (ORC-VCR) system.
  • ORC-VCR organic Rankine and vapor compression refrigeration
  • the Rankine cycle of system 1000 includes expansion device 102.
  • Expansion device 102 may be, for example and without limitation, a turbine.
  • expansion device 102 may be replaced with another system or apparatus capable of producing work from thermal energy and/or converting thermal energy to another form of energy.
  • the Rankine cycle of system 1000 also includes condenser 104.
  • Condenser 104 is downstream of and operative ly and fluidly coupled to expansion device 102.
  • condenser 104 may be replaced with another heat sink system or apparatus.
  • the Rankine cycle of system 1000 includes first heat exchanger 116.
  • First heat exchanger 1 16 is upstream of, operative ly coupled with, and fluidly coupled with expansion device 102.
  • first heat exchanger may be any of a variety of heat exchanges suitable for providing for thermal energy transfer between, e.g., working fluids.
  • the Rankine cycle of system 1000 also includes second heat exchanger 118.
  • Second heat exchanger 1 18 is upstream of and operatively and fluidly coupled to first heat exchanger 116. Also, second heat exchanger is downstream of and operatively and fluidly coupled to condenser 104. As shown, second heat exchanger 118 is operatively fluidly coupled to condenser 104 via pump 106.
  • second heat exchanger may be any of a variety of heat exchanges suitable for providing for thermal energy transfer between, e.g., working fluids.
  • First heat exchanger 116 of the Rankine cycle of system 1000 is operatively and thermally coupled to primary waste heat source 100, such that working fluid within first heat exchanger 1 16 is positioned to exchange thermal energy with exhaust 120 of heat source 100.
  • primary waste heat source 100 may be the exhaust 120 of an internal combustion engine (ICE), such as the exhaust of a CCHP or CHP system.
  • ICE internal combustion engine
  • exhaust enters first heat exchanger 116 as relatively hot exhaust 120 and exits first heat exchanger 1 16 as at least partially cooled exhaust 120, due to the transfer of thermal energy from the exhaust to working fluid 101a flowing through first heat exchanger 1 16.
  • the Rankine cycle is, thus, composed of condenser 104, pump 106, and expander 102 in a closed loop cycle, and is thermally coupled via one or more heat exchanges with the VCR cycle and the engine of a CCHP.
  • the vapor compression refrigeration (VCR) cycle of system 1000 includes compressor 114.
  • Compressor 1 14 is downstream of and operatively and fluidly coupled to evaporator 1 12.
  • Evaporator 1 12 is downstream of and operatively and fluidly coupled to condenser 108. As shown, evaporator 1 12 is operatively and fluidly coupled to condenser 108 via expansion valve 110.
  • VCR cycle of system 1000 is operatively and thermally coupled to the Rankine cycle of system 1000 via second heat exchanger 1 18, which is positioned between condenser 108 and compressor 114.
  • Condenser 108 is downstream of and operatively and fluidly coupled to second heat exchanger 118, and compressor 114 is upstream of and operatively and fluidly coupled to second heat exchanger 1 18.
  • VCR is compos3ed of condenser 1 18, expansion valve 1 10, evaporator 1 12, and compressor 1 14 in a closed loop cycle, and is thermally coupled with ORC via second heat exchanger 1 18.
  • the VCR and engine in some aspects, form a CCHP system.
  • waste heat is removed from a target environment via evaporator 1 12.
  • the thermal energy of waste heat is transferred to working fluid 101b within and flowing through evaporator 1 12.
  • Working fluid 101b then flows from evaporator 1 12, through compressor 1 14, and then through second heat exchanger 1 18. Within second heat exchanger 1 18, thermal energy of working fluid 101b is transferred from working fluid 101b to working fluid 101a. Working fluid 101b is discharged to condenser 108 under pressure provided by compressor 1 14. Working fluid 101b then flows from condenser 108, through expansion valve 1 10, and back into evaporator 1 12, wherein the vapor compression refrigeration cycle begins again. Thus, heat from the working fluid of the VCR, 101b, preheats the working fluid of the ORC, 101a.
  • Waste heat 120 (e.g. , heated exhaust) flows from primary waste heat source 100, through first heat exchanger 1 16. Heat transferred from waste heat 120 to preheated working fluid 101a, within first heat exchanger 1 16, evaporating working fluid 101 a and cooling waste heat to form cooled exhaust 120. Evaporated working fluid 101a enters expansion device 102, and expands therein, producing work within expansion device 102.
  • the expansion device 102 may be, for example, a turbine generator, such that expansion of working fluid 101a therein drives the turbines, generating electricity via methods known to those skilled in the art.
  • Working fluid 10 la then flows from expansion device 102 into condenser 104. Within condenser 104, working fluid 101a is condensed and cooled.
  • working fluid 101a flows form condenser 104 into second heat exchanger 1 18 for preheating.
  • Pump 106 recycles working fluid 101a from condenser 104 through second heat exchanger 1 18, and into first heat exchanger 1 16, where the Rankine cycle begins again. While heat exchangers 1 16 and 1 18 are shown as separate heat exchangers, in some aspects a single heat exchanger is used in place of heat exchangers 1 16 and 1 18 to provide the functions of both heat exchangers 1 16 and 1 18.
  • the working fluid of the ORC is an organic working fluid.
  • the working fluid of the ORC may be olefin-based, hyrdrofluoroolefin-based, or hydrofluorocarbon-based.
  • the working fluid may be R-134a (1, 1 , 1 ,2- tetrafluoroethane); R-245fa (pentafluoropropane); a hydrofluoroolefin (HFO), such as DR-2 which is also referred to as R-1336mzz(Z) or (Z)-l, l, l,4,4,4-hexafluoro-2-butene, or an HFO such as DR-40A which is a blend of a hydrofluorocarbon and an HFO in a near azeotropic proportion.
  • HFO hydrofluoroolefin
  • the working fluid of the ORC has a molecular mass that is greater than about 100 g/mol, greater than about 105 g/mol, greater than about 1 10 g/mol, greater than about 120 g/mol, greater than about 130 g/mol, greater than about 140 g/mol, greater than about 150 g/mol, or greater than about 160 g/mol.
  • the working fluid of the ORC has a boiling point that is greater than about -25 °C, greater than about 0 °C, greater than about 10 °C, greater than about 15 °C, greater than about 20 °C, or greater than about 30 °C.
  • the working fluid of the ORC is non-flammable, has low toxicity, has a low global warming potential (GWP), or combinations thereof.
  • the working fluid of the ORC has a high stability and compatibility with available lubricants and with common materials of equipment construction.
  • the working fluid of the VCR may be R-410A (a mixture of difluoromethane and pentafluoroethane).
  • the thermal efficiency of the ORC ranges from 1 to 15 %, or from 2 to 14%, or from 3 to 13%, or from 4 to 12%, or from 5 to 1 1 %, or from 6 to 10%, or from 7 to 9%. In some aspects, the thermal efficiency of the ORC is greater than 9%, greater than 10%, greater than 1 1 %, greater than 12%, greater than 13%, greater than 14%, greater than 15%, or greater than 16%.
  • the coefficient of performance (COP) of the VCR ranges from 3 to 17, or from 4 to 16, or from 5 to 15, or from 6 to 14, or from 7 to 13, or from 8 to 12, or from 9 to 1 1.
  • the COP of the overall system ranges from 0.5 to 3, or from 1 to 2.5, or from 1.5 to 2.
  • the adiabatic efficiency of the expander is at least 75% or at least 90%. Examples
  • FIG. 2 is a mass flow and energy analysis of a ORC-VCR system in which working fluid 101a is R-134a ( 1, 1, 1,2-tetrafluoroethane) and working fluid 101b is R-410A (a mixture of difluoromethane and pentafluoroethane).
  • working fluid 101a is R-134a ( 1, 1, 1,2-tetrafluoroethane)
  • working fluid 101b is R-410A (a mixture of difluoromethane and pentafluoroethane).
  • the primary heat source 100 is an internal combustion CHP system generating 51.21kW of energy with an electrical power output of 12kW and a heat output of 28.8kW. All, or at least some of, the heat output of all of primary heat source 100 is transferred to the Rankine cycle of system 1000.
  • the exhaust 120 was flowing into evaporator 1 16 at a rate of 104.22 kg/h and exited the evaporator 1 16 at a reduced temperature of 80 °C.
  • Temperatures, pressures, and flow rates of working fluids 101a and 101b are indicated along the flow paths thereof shown in FIG. 2, along with other parameters of system 1000 utilized in Example 2.
  • Working fluid 101a exited evaporator 1 16 at a temperature of 71.80 °C, a pressure of 20.2 barg, and a flow rate of 6.49 m 3 /h. Within expander 102, 2.34 kW of power were produced at an adiabatic efficiency of 90%.
  • the working fluid 101a exited expander 102 at a temperature of 43.27 °C and a pressure of 10 barg, and entered condenser 104, where heat flow was equal to 33.2.
  • Working fluid 101a exited the condenser 104 at a temperature of 40 °C and a pressure of 9.8 barg and entered pump 106 (at a power of 0.25 kW).
  • Working fluid 101a exited pump 106 at a temperature of 41.14 °C and a pressure of 20.6 barg, and entered second heat exchanger 1 18, where 6.5 kW is supplied from the R-410A refrigeration cycle loop to the ORC via heat exchanger 1 18.
  • Working fluid 101a exited second heat exchanger 1 18 at a temperature of 60.4 °C and a pressure of 20.4 barg and entered first heat exchanger 1 16.
  • Working fluid 10 la had a flow rate of 705 kg/h within the ORC.
  • the flow rate of R-410a within the VCR was 612.8 kg/h.
  • Working fluid 101b exited evaporator 1 12 (heat flow of 28.1 kW) at a temperature of 12.8 °C, a pressure of 8.1 barg, and a flow rate of 18.9 m 3 /h, and entered compressor 1 14. Within compressor 1 14, 6.5 kW of power were consumed at an adiabatic efficiency of 84%.
  • the working fluid 101b exited compressor 1 14 at a temperature of 78.9 °C and a pressure of 26.5 barg and entered second heat exchanger 1 18.
  • Working fluid 101b exited second heat exchanger 1 18 at a temperature of 47 °C and a pressure of 26.3 barg and entered condenser 108 (heat flow equal to 34.7 kW).
  • Working fluid 101a exited condenser at a temperature of 40 °C and a pressure of 26.1 barg, entered expansion valve 1 10, and exited expansion valve 1 10 at a temperature of 6.8 °C and a pressure of 8.5 barg.
  • FIG. 4 is an enthalpy chart of the ORC-VCR system of FIG. 2.
  • the saturation pressure was 9.8 barg. Consequently, the gas (evaporated working fluid 101a) in Example 2 is only capable of being expanded to 10 barg, limiting the work produced in expanding device 102.
  • the temperature of evaporator (first heat exchanger 1 16) is 70 °C, so that the temperature difference between the high and low stage of the Rankine cycle is not sufficient, affecting the efficiency of the Rankine cycle.
  • the mass heat of evaporation of R- 134a is high, so that a high amount of refrigerant is required for the process, increasing the size of pipes and equipment, as well as the cost of the cycle.
  • R-134a was replaced with R-245fa (pentafluoropropane), an organic refrigerant that is heavier (i. e. , has a higher molecular mass) than R-134a.
  • R-245fa penentafluoropropane
  • R-134a an organic refrigerant that is heavier (i. e. , has a higher molecular mass) than R-134a.
  • Working fluid 101a exited evaporator 1 16 at a temperature of 126 °C and pressure of 20.2 barg. Within expander 102, 5.36 kW of power were produced at an adiabatic efficiency of 90%. The working fluid 101a exited expander 102 at a temperature of 65 °C and a pressure of 2.7 barg, and entered condenser 104, where heat flow was equal to 29.8. Working fluid 101a exited the condenser 104 at a temperature of 40 °C and a pressure of 2.5 barg and entered pump 106 (at a power of 0.21 kW).
  • Working fluid 101a exited pump 106 at a temperature of 41 °C and a pressure of 20.6 barg, and entered second heat exchanger 1 18, where 6.5 kW is supplied from the R-41 OA refrigeration cycle loop to the ORC via heat exchanger 1 18.
  • Working fluid 101a exited second heat exchanger 1 18 at a temperature of 80 °C and a pressure of 20.4 barg and entered first heat exchanger 116.
  • Working fluid had a flow rate of 536.2 kg/h within the ORC.
  • FIG. 5 is an enthalpy chart of the ORC-VCR system of FIG. 3
  • R-245fa is a suitable refrigerant for the Rankine cycle of system 1000, as the thermal efficiency obtained was almost three times higher than the thermal efficiency obtained using R-134a as working fluid 101a, in Example 1.
  • R-245fa may be a more suitable refrigerant for the Rankine cycle of system 1000 because at a condenser 104 temperature of 40 °C, the saturation pressure is 2.5 barg. Therefore, the gas (evaporated working fluid 101a) can be expanded to a lower pressure in expansion device 102, such that more work is produced in expansion device 102.
  • the high temperature of the Rankine cycle is 126 °C, so that there is a high temperature difference between the upper and lower stages of the Rankine cycle, thereby increasing the thermal efficiency of system 1000.
  • the mass heat of vaporization of R-245fa is lower than that of R-134a, a smaller amount of refrigerant is needed in the Rankine cycle, such that the size of pipes and equipment of system 1000 may be reduced, with a corresponding reduction in capital costs for constructing system 1000.
  • Table 1 lists the general system and subsystem efficiencies for the various configurations, where HX represents the ORC-VCR heat exchanger (second heat exchanger 118).
  • HFOs hydrofluoroolefins
  • ORC Organic Rankine Cycle
  • HFOs are non-flammable, have low toxicity, and have low global warming potential (GWP).
  • GWP global warming potential
  • HFOs have high stability and compatibility with available lubricants and with common materials of equipment construction. Use of HFOs as a refrigerant in the ORC may increase the thermal efficiency of the ORC.
  • DR-2 is a refrigerant, also known as R- 1336mzz(Z), that has a substantially lower GWP than R-245fa. DR-2 is also less toxic than R-245fa. Furthermore, in the Mollier diagram for DR-2, the slopes of the saturated vapor lines allow the operation of the expander (e.g. , expander 102) at any degree of vapor superheat without condensation occurring. This is evident in view of FIGS. 8 and 9.
  • the expander e.g. , expander 102
  • DR-40A is blend of a hydrofluorocarbon (HFC) refrigerant and an HFO in a near azeotropic proportion.
  • HFC hydrofluorocarbon
  • Use of DR-2 in the ORC provides the ORC with a lower operating pressure than does use of DR-40A in the ORC, because DR-2 has a higher normal boiling temperature than DR-40A, which is a relevant design consideration for systems having high condensing temperatures.
  • Example 3 is now described.
  • the refrigerant DR-2 was not evaluated in Example 3.
  • the refrigerant DR-40A was not evaluated in Example 3.
  • a heat flow of 28.84 kW is transferred from the exhaust gas stream 100 of an internal combustion system to the evaporator 1 16 of the ORC.
  • the exhaust gas stream 100 was at a flow rate of 104.22 kg/h.
  • the exhaust gas existed as waste heat 120, at a temperature of 80 °C.
  • 6.5 kW is supplied from the R-410A refrigeration cycle loop to the ORC via heat exchanger 1 18.
  • the power consumed by the fan of the condenser 104 of the ORC was 0.3 kW.
  • the adiabatic efficiency for the pump 106 and the expander 102 is 50% and 75%, respectively.
  • the lower pressure of the ORC was established as the saturation pressure at 40 °C of the refrigerant, as air is used as cooling fluid in the condenser.
  • a pressure drop of 0.2 bar was considered in the heat exchangers, such as the condenser 104 and the evaporator 1 16.
  • working fluid 101a exited evaporator 1 16 at a temperature of 155 °C and pressure of 20.2 barg. Within expander 102, 4.86 kW of power were produced at an adiabatic efficiency of 75%.
  • the working fluid 101a exited expander at a temperature of 91 °C and a pressure of 2.7 barg, and entered condenser 104, where heat flow was equal to 31.07.
  • Working fluid 101a exited the condenser 104 at a temperature of 40 °C and a pressure of 2.5 barg and entered pump 106 (at a power of 0.44 kW and an efficiency of 50%).
  • Working fluid 101a exited pump 106 at a temperature of 42 °C and a pressure of 20.6 barg, and entered second heat exchanger 1 18, where 6.5 kW is supplied from the R-410A refrigeration cycle loop to the ORC via heat exchanger 1 18.
  • Working fluid 101a exited second heat exchanger 1 18 at a temperature of 78 °C and a pressure of 20.4 barg and entered first heat exchanger 1 16.
  • Working fluid 101a had a flow rate of 530.1 kg/h within the ORC.
  • working fluid 101a exited evaporator 1 16 at a temperature of 178 °C and pressure of 30.2 barg. Within expander 102, 5.72 kW of power were produced at an adiabatic efficiency of 75%. The working fluid 101a exited expander at a temperature of 95 °C and a pressure of 2.7 barg, and entered condenser 104, where heat flow was equal to 30.18. Working fluid 101a exited the condenser 104 at a temperature of 40 °C and a pressure of 2.5 barg and entered pump 106 (at a power of 0.64 kW and an efficiency of 50%).
  • Working fluid 101a exited pump at a temperature of 42 °C and a pressure of 30.6 barg, and entered second heat exchanger 1 18, where 6.5 kW is supplied from the R-410A refrigeration cycle loop to the ORC via heat exchanger 1 18.
  • Working fluid 101a exited second heat exchanger 1 18 at a temperature of 78 °C and a pressure of 30.4 barg and entered first heat exchanger 1 16.
  • Working fluid had a flow rate of 508.9 kg/h within the ORC.
  • the ORC was optimized by varying the discharge pressure of the pump 106, as the lower pressure of the ORC is limited by the air temperature (40 °C). Based, on the pressure- enthalpy diagram of DR-2, the critical pressure of the refrigerant is 2.9 MPa, such that at higher pressures a supercritical cycle is obtained. The inlet pressure of the expander 102 was changed to 3 MPa, obtaining the cycle parameters shown in Figure 7. In FIG. 9, the Mollier diagram for the optimized Rankine cycle with DR-2 is included.
  • DR-2 is a suitable refrigerant for the ORC, as the ORC becomes more thermally efficient and more work is produced during the expansion in comparison to use of R-245fa. Also, DR-2 is less toxic and has a lower global warming potential than R-245fa, having more environmental benefits as well as less safety hazards.
  • some aspects of the present disclosure relate to a method that includes generating mechanical energy 5000 using engine 100.
  • a portion of the mechanical energy 5000 may be transmitted to a vapor compression refrigeration (VCR) cycle 6000.
  • VCR vapor compression refrigeration
  • mechanical energy 5000 may drive the compressor of the VCR cycle 6000 ⁇ e.g. , compressor 1 14).
  • the mechanical energy 5000 is converted into electrical energy prior to driving the compressor of the VCR cycle 6000, such as via a generator (e.g. , generator 7000 ).
  • United States Patent Application No. 15/629,864 provides relevant background disclosure with regards to driving the compressor of a refrigeration cycle loop using an internal combustion engine and is incorporated herein by reference for ail purposes and made a part of the present disclosure.
  • Engine 100 may be operatively coupled with the compressor of the VCR cycle 6000 and may drive the compressor in the same or a substantially similar manner as is described in United States Patent Application No. 15/629,864.
  • a portion of the mechanical energy 5000b produced by engine 100 may be transmitted to a generator 7000 configured to convert the mechanical energy 5000b into electrical energy 5004, such as for providing electricity to a local environment, such as house 8000.
  • Engine 100 produces waste heat as thermal energy 5002. At least a portion of thermal energy 5002 is transferred to ORG 9000, where the thermal energy is converted into electrical and/or mechanical energy 5006, as described elsewhere herein.
  • the method includes providing air conditioning to the local environment 8000 using the VCR cycle 6000.
  • the conditioned air 5010 may be transmitted into an interior of house 8000.
  • the VCR cycle 6000 produces waste heat as thermal energy 5012.
  • the method includes transferring at least a portion of the thermal energy 50 2 of waste heat produced by the VCR cycle 6000 into a working fluid of a ORC 9000, where the thermal energy is converted into electrical and/or mechanical energy 5006, as described elsewhere herein.
  • the engine 100 is an internal combustion engine, and the engine 100 and the VCR cycle 600 are components of a single combined cooling, heating, and power system (CCHP) 1001.
  • CCHP cooling, heating, and power system
  • the electrical and/or mechanical energy produced by the OCR 9000 may be transmitted to the local environment for providing power, or transmitted to another device.
  • the local environment is a substantially enclosed building having an air conditioning and ventilation unit for supplying cooled air within the building.
  • a "local environment" may be defined as a discrete space with quantifiable energy demands, including thermal and/or electrical energy demands.
  • the local environment may be a residence, building, mobile enclosure or other facility or interior space thereof. It will become apparent to one skilled in the relevant engineering, architecture, or other technical art, that these aspects in part, or in their entirety, may be equally applicable to other settings and other applications.

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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

Un procédé d'augmentation de l'efficacité d'un système combiné de refroidissement/chauffage et de puissance (CCHP) consiste à utiliser un générateur à cycle de Rankine organique pour exploiter la chaleur perdue du système CCHP et de refroidissement. La chaleur perdue du moteur CCHP est transférée au cycle de Rankine par l'intermédiaire d'un échangeur de chaleur, permettant un transfert de chaleur sensible, du moteur au fluide de travail du cycle de Rankine, par l'intermédiaire de la convection de l'énergie interne de gaz brûlé de combustion et/ou de la conduction de chaleur à travers le matériel de support de moteur par l'intermédiaire d'un premier dispositif échangeur de chaleur. Le sous-système de refroidissement dudit système CCHP est un cycle de réfrigération par compression de vapeur (VCR). La chaleur perdue émanant du cycle VCR est transférée du fluide de travail du cycle VCR au fluide de travail du cycle de Rankine par convection par l'intermédiaire d'un second dispositif échangeur de chaleur.
PCT/US2018/029627 2017-04-26 2018-04-26 Procédés, systèmes et appareil de production d'énergie, de réfrigération et de récupération de chaleur perdue combinées WO2018200856A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112012806A (zh) * 2020-08-31 2020-12-01 董荣华 大型制冷机组余热发电系统
EP4269757A1 (fr) * 2022-04-28 2023-11-01 Borealis AG Procédé de récupération d'énergie

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040088992A1 (en) * 2002-11-13 2004-05-13 Carrier Corporation Combined rankine and vapor compression cycles
US20090211253A1 (en) * 2005-06-16 2009-08-27 Utc Power Corporation Organic Rankine Cycle Mechanically and Thermally Coupled to an Engine Driving a Common Load
US20110296849A1 (en) * 2010-06-02 2011-12-08 Benson Dwayne M Integrated power, cooling, and heating apparatus utilizing waste heat recovery
US20150047351A1 (en) * 2011-09-30 2015-02-19 Takayuki Ishikawa Waste heat utilization apparatus

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040088992A1 (en) * 2002-11-13 2004-05-13 Carrier Corporation Combined rankine and vapor compression cycles
US20090211253A1 (en) * 2005-06-16 2009-08-27 Utc Power Corporation Organic Rankine Cycle Mechanically and Thermally Coupled to an Engine Driving a Common Load
US20110296849A1 (en) * 2010-06-02 2011-12-08 Benson Dwayne M Integrated power, cooling, and heating apparatus utilizing waste heat recovery
US20150047351A1 (en) * 2011-09-30 2015-02-19 Takayuki Ishikawa Waste heat utilization apparatus

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112012806A (zh) * 2020-08-31 2020-12-01 董荣华 大型制冷机组余热发电系统
EP4269757A1 (fr) * 2022-04-28 2023-11-01 Borealis AG Procédé de récupération d'énergie
WO2023208978A1 (fr) * 2022-04-28 2023-11-02 Borealis Ag Procédé de récupération d'énergie

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