WO2022037711A1 - 一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站及其调节方法 - Google Patents

一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站及其调节方法 Download PDF

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Publication number
WO2022037711A1
WO2022037711A1 PCT/CN2021/121402 CN2021121402W WO2022037711A1 WO 2022037711 A1 WO2022037711 A1 WO 2022037711A1 CN 2021121402 W CN2021121402 W CN 2021121402W WO 2022037711 A1 WO2022037711 A1 WO 2022037711A1
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Prior art keywords
seawater
way valve
heat
flasher
cycle
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PCT/CN2021/121402
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English (en)
French (fr)
Inventor
蔺新星
尹立坤
王倩
苏文
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中国长江三峡集团有限公司
中南大学
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Priority claimed from CN202023213436.9U external-priority patent/CN214660401U/zh
Priority claimed from CN202011578173.3A external-priority patent/CN112627925B/zh
Application filed by 中国长江三峡集团有限公司, 中南大学 filed Critical 中国长江三峡集团有限公司
Priority to US18/258,832 priority Critical patent/US12253011B2/en
Publication of WO2022037711A1 publication Critical patent/WO2022037711A1/zh

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    • 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
    • F01K25/103—Carbon dioxide
    • 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
    • F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
    • 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
    • F01K13/00—General layout or general methods of operation of complete plants
    • 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
    • F01K23/064—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 in combination with an industrial process, e.g. chemical, metallurgical
    • 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
    • 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
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/32—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines using steam of critical or overcritical pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the invention belongs to the technical field of thermal energy power and seawater desalination, and relates to a comprehensive utilization system of thermal energy, in particular to a flexible thermal power system based on supercritical carbon dioxide (S-CO 2 ) cycle and a multi-stage seawater desalination system based on energy cascade utilization, The constituted high flexibility electricity and water combined production system and operation method.
  • S-CO 2 supercritical carbon dioxide
  • the high proportion of clean energy connected to the grid is the general situation of foreign energy production and consumption.
  • the current energy storage configuration scale is too low to achieve a comprehensive adjustment of the power system, requiring a large number of thermal power stations to participate in the adjustment.
  • highly flexible thermal power plants will coexist with other clean energy sources for a long time as the most basic adjustment measure.
  • the turbine used In order to make full use of steam energy in the steam power cycle, the turbine used generally adopts multi-stage expansion, especially with the decrease of steam pressure and density during the expansion process, the size of the impeller increases step by step. At this stage, the high-efficiency steam turbine can reach grade 50 or above, and the size and thermal inertia are huge, which is not conducive to adjustment.
  • a low-pressure pumping method has to be adopted, sacrificing a lot of useful energy.
  • the critical point of CO2 is lower, and the supercritical state is easy to achieve.
  • the thermodynamic properties of CO2 have many advantages.
  • heat transfer performance its density is close to that of liquid, and its heat transfer efficiency is high; in terms of dynamic performance: its viscosity is close to that of gas, easy to diffuse, and has strong fluidity and strong workability.
  • the S- CO2 performance characteristics make the S- CO2 Brayton cycle adaptable to a wider temperature range and higher system cycle efficiency.
  • the S- CO2 Brayton cycle is compact, small and light in weight. Under the condition of the same power generation capacity, the turbine size is 1/30 of that of the steam power generation system.
  • the S-CO 2 Brayton cycle has more advantages in terms of rapid start-up, emergency response and energy utilization efficiency, especially if it is used as a peak-shaving power station, its operating economic advantage is significantly higher than that of the steam cycle, and it is expected to become the next generation of efficient and economical technology.
  • Thermal power generation technology
  • thermodynamic processes such as recuperation, reheating, staged compression, and intercooling are applied to the S- CO2 Brayton cycle, from which the S- CO2 Brayton cycle is derived.
  • Various improvements are applied to the S- CO2 Brayton cycle, from which the S- CO2 Brayton cycle is derived.
  • most of the circulation structures are in a fixed form. Due to the high degree of tight coupling between each process link, the flow adjustment and the split ratio adjustment are the main adjustments to the system. This also results in a limited range of system adjustment, which does not fully exploit the turbine's high-efficiency performance and flexibility potential.
  • the heat release process of the system will also fluctuate in a wide range, and a large amount of low-grade heat energy will be generated correspondingly.
  • the thermal cycle seawater desalination process is a good flexible load, and the coordinated implementation in the early stage of the construction of a new thermal power station can effectively improve the energy efficiency and economy of the system.
  • Seawater desalination technology is an important way of freshwater production in the future.
  • the technology of adding multi-stage flashing seawater desalination devices at the end of the thermoelectric production process is relatively mature.
  • simply adding a seawater desalination process at the end of the traditional thermal power cycle process cannot meet the actual needs.
  • the flexibility of the thermodynamic cycle itself needs to be improved, and the matching seawater desalination process should also be integrated. If the new S- CO2 power cycle process is used for power generation, the exhaust gas temperature of the boiler will be greatly reduced, so the cycle thermal efficiency on the desalination side needs to be further improved to reduce the cost of the whole life cycle of the seawater desalination process.
  • the invention is based on an integrated process of supercritical carbon dioxide power cycle combined with seawater desalination to reduce the exhaust temperature of the heat source, improve the thermal efficiency of the thermal power cycle, and improve the flexibility and adjustability of the output of the thermal power station;
  • the utilization efficiency of the heat source in the desalination process makes it a standing "flexible load" of the power station, further improving the overall efficiency and flexibility of the system.
  • the purpose of the present invention is to achieve in this way: a flexible power plant based on supercritical carbon dioxide power cycle combined with seawater desalination, which includes a heat source cycle system, a thermodynamic cycle system, a seawater desalination system and a control system ;
  • the heat source circulation system is connected with the thermodynamic circulation system and the seawater desalination system, and respectively provides the heat sources required in the working process for them;
  • the control system is simultaneously connected with the various executive agencies of the heat source circulation system, the thermodynamic circulation system and the seawater desalination system, and controls their corresponding work.
  • the heat source circulation system includes a boiler, a heat storage tank, a CO2 heater, a CO2 preheater, a seawater heater, the second bypass valve, the sixth three-way valve, the seventh three-way valve, and the eighth three-way valve , the ninth three-way valve, the thirteenth valve, the eleventh three-way valve, the twelfth three-way valve, the thirteenth three-way valve, the first intermediate pump, the second intermediate pump and supporting management ;
  • the boiler is the original heat source of the system, the boiler is connected in series with the CO 2 heater and the CO 2 preheater, and provides heat for the thermodynamic circulation system; the boiler is connected with the seawater heater and provides heat for the seawater desalination system;
  • the heat storage tank is connected in parallel on both sides of the series heat exchanger group formed by the CO 2 heater and the CO 2 preheater to adjust the thermal inertia of the boiler and the load of the CO 2 heater and the CO 2 preheater during the heat exchange process of the boiler.
  • the first intermediate working fluid pump and the second intermediate working fluid pump are respectively connected with the thermodynamic circulation system and the heat storage tank, and are respectively used to adjust the flow distribution of the heating thermodynamic circulation system and the heat storage tank;
  • the twelfth The three-way valve, the thirteenth three-way valve and the second bypass valve are connected in parallel with the second intermediate working fluid pump, and realize the heat absorption and release of the heat storage tank and the flow regulation;
  • the eighth three-way valve and the ninth three-way valve are used to bypass the high temperature side of the CO 2 heater, and the thirteenth and eleventh three-way valves are used to bypass the high temperature side of the CO 2 preheater.
  • a wide range of flexible control of the thermodynamic cycle is achieved.
  • the heat storage material of the heat storage tank is made of molten salt or liquid metal. According to the requirements of the power system, when the system load drops and the boiler heat cannot be quickly adjusted, part of the heat is stored in the heat storage tank. When the system load increases, the boiler heat cannot be quickly adjusted. When , it is proposed that the heat stored in the heat storage tank is supplementary heat for the power cycle;
  • the CO2 heater, CO2 preheater and seawater heater are directly built-in and installed in the boiler, removing the intermediate medium to directly heat CO2 or seawater.
  • the thermodynamic cycle system includes a CO2 heater, a CO2 preheater, a primary expander, a secondary expander, a primary compressor, a secondary compressor, a primary regenerator, a secondary regenerator, CO2 cooler, first bypass valve, first three-way valve, second three-way valve, third three-way valve, fourth three-way valve, fifth three-way valve and supporting pipelines;
  • thermodynamic cycle system uses CO 2 as the working medium, which is nested with two-stage supercritical CO 2 Brayton cycle: including one-stage supercritical CO 2 Brayton cycle and two-stage supercritical CO 2 Brayton cycle; CO 2
  • the heater provides heat for the first-stage supercritical CO 2 Brayton cycle, and then provides heat for the second-stage supercritical CO 2 Brayton cycle through the CO 2 preheater, and the amount of the first-stage and second-stage supercritical CO 2 Brayton cycles are indirectly combined with cascade utilization of energy.
  • the circulating working medium of the first-stage supercritical CO 2 Brayton cycle is supercritical CO 2 , and the CO 2 working medium successively flows through the first-stage compressor, the low-temperature side of the second-stage regenerator, the low-temperature side of the first-stage regenerator, and CO. 2 heater low temperature side, primary expander, primary regenerator high temperature side, first three-way valve, secondary regenerator high temperature side, second three-way valve, CO2 cooler high temperature side, primary compressor After completing the cycle, the corresponding CO 2 fluid has undergone several processes of boosting, endothermic, endothermic, endothermic, expansion, exothermic, confluence, exothermic, shunt, exothermic, and boosting to achieve endothermic and workmanship. the overall process flow;
  • the circulating working fluid of the secondary supercritical CO 2 Brayton cycle is supercritical CO 2 , and the CO 2 working fluid successively flows through the secondary compressor, the low temperature side of the CO 2 preheater, the secondary expander, the first tee The valve, the high temperature side of the secondary regenerator, the second three-way valve, and the secondary compressor complete the cycle.
  • Each process realizes the overall process flow of heat absorption and workmanship;
  • the first-level and second-level supercritical CO2 Brayton cycles realize the direct mutual combination of the above-mentioned first-level and second-level supercritical CO2 Brayton cycles through the first three-way valve, the second three-way valve and the second-level regenerator , through the first three-way valve and the second three-way valve to adjust the split ratio of the secondary cycle to adjust the system operation;
  • the first three-way valve, the second three-way valve and the first bypass valve are used to bypass the secondary supercritical CO2 Brayton cycle so that the primary supercritical CO2 Brayton cycle operates independently, and the third and third The through valve, the fourth three-way valve and the fifth three-way valve are used to bypass the primary supercritical CO2 Brayton cycle to make the secondary supercritical CO2 Brayton cycle operate independently;
  • the first-stage expander, the second-stage expander, the first-stage compressor, and the second-stage compressor adopt the link mode of transmission and clutch to meet the adjustment conditions; CO 2 heater, CO 2 preheater, and first-stage regenerator , Secondary regenerator, CO2 cooler using printed circuit board heat exchanger.
  • the seawater desalination system includes CO2 cooler, seawater heater, seawater preheater, steam condenser, primary flasher, middle flasher, final flasher, fresh water storage tank, fourteenth three-way valve, tenth Five three-way valve, sixteenth three-way valve, seventeenth three-way valve, fresh water pump, first sea water pump, second sea water pump, third sea water pump, fourth sea water pump and supporting pipelines;
  • the seawater heater, seawater preheater and steam condenser use shell-and-tube heat exchangers with strong anti-corrosion blocking, strong plugging ability, low pressure requirements and good economy.
  • the heat exchange tube bundles in the heat exchanger are made of copper. Tube;
  • the heat for heating seawater comes from three parts, including the recovery of condensation heat carried after seawater flashing through the steam condenser, the intermediate flasher and the primary flasher, the recovery of the heat of cooling at the end of the thermodynamic cycle through the seawater preheater, and the recovery of the heat of condensation at the end of the thermodynamic cycle through the seawater heater. Recover the waste heat of flue gas in the heat source cycle, in which the softened water is used to flow through the fresh water pump, the low temperature side of the CO 2 cooler, the high temperature side of the seawater preheater, and the fresh water pump, and the cycle of pressure boosting, heat absorption, heat release and pressure boosting is completed correspondingly.
  • the heat released by the cooling at the end of the thermodynamic cycle is indirectly transferred to the seawater, in which the softened water cycle is mainly used to protect the printed circuit board heat exchanger used in the CO2 cooler, or a simplified system is used.
  • the device directly uses the cooling heat at the end of the power cycle to heat the seawater;
  • the naturally extracted low-temperature seawater flows through the low-temperature side of the steam condenser, the low-temperature condenser in the middle-stage flasher, the low-temperature condenser in the primary flasher, the first seawater pump, the fourteenth three-way valve, and the low-temperature seawater preheater.
  • the seawater tank and the fourth seawater pump are discharged to complete seawater concentration, and the corresponding seawater fluid has experienced endothermic, endothermic, endothermic, pressure boosting, shunt, endothermic, endothermic, flash concentration, pressure boost, and flash concentration.
  • boosting, capacity expansion flash evaporation concentration, boost discharge several processes to realize the process flow of endothermic low pressure flash evaporation concentration.
  • the primary flasher is composed of five parts: a first shell, a first low-temperature condenser, a first condensate pan, a first seawater tank, and a second seawater pump.
  • the primary flasher includes a first low-temperature seawater inlet, a first The low temperature seawater outlet, the first water vapor outlet, the first fresh water outlet, the first high temperature seawater inlet and the first high temperature seawater outlet have six interfaces, wherein the first seawater tank is stacked with pebbles to increase the gas outlet speed, and the first condensed water The bottom of the pan leads out the first fresh water outlet to discharge the condensed water;
  • the water vapor flashed in the primary flasher is condensed into fresh water by contacting the first low-temperature condenser in the primary flasher, and collected by the first condensed water tray in the primary flasher, and finally condensed into the freshwater storage tank, and the remaining steam flows into the fresh water storage tank.
  • the middle-stage flasher is mixed with the water vapor flashed in the middle-stage flasher, contacted with the low-temperature condenser in the middle-stage flasher and condensed into fresh water, which is collected by the second condensate tray in the middle-stage flasher and finally converged to the freshwater storage tank.
  • the remaining steam is mixed with the water vapor from the expansion and flashing in the final stage flasher through the fifteenth three-way valve and enters the high temperature side of the steam condenser to release heat and condense, and finally flows into the fresh water storage tank;
  • the middle-stage flasher is composed of five parts: a second shell, a second low-temperature condenser, a second condensate pan, a second seawater tank, and a third seawater pump.
  • the middle-stage flasher includes a second low-temperature seawater inlet, a second The low temperature seawater outlet, the second water vapor outlet, the second fresh water outlet, the second high temperature seawater inlet and the second high temperature seawater outlet have six interfaces, wherein the second seawater tank is stacked with pebbles to increase the gas outlet speed, and the second condensate water A second fresh water outlet is drawn from the bottom of the pan to discharge condensed water.
  • the number of the middle flasher can be increased or decreased according to the needs of the seawater desalination process, and the second seawater tank in the middle flasher can be installed according to the needs of the seawater desalination process.
  • the gas waste heat recovery device is used to utilize the flue gas discharged from the high temperature side of the seawater heater.
  • the last-stage flasher is composed of a third shell, a fan, a water distributor, a grille, a third seawater tank, and a third seawater pump, and the fan is used to increase the disturbance and improve the seawater evaporation speed on the surface of the grille;
  • the fresh water storage tank adopts a sealed cabin, and the upper part is equipped with an exhaust valve for regular vacuuming to provide negative pressure for the fresh water side of the seawater desalination process;
  • the number of the middle-stage flashers can be increased or decreased according to the evaporation volume required by the process, and the fifteenth three-way valve, the sixteenth three-way valve, and the seventeenth three-way valve are used to bypass the final-stage flasher.
  • the control system includes a first three-way valve, a second three-way valve, a third three-way valve, a fourth three-way valve, a fifth three-way valve, a sixth three-way valve, a seventh three-way valve, and an eighth three-way valve.
  • the system selects working mode one:
  • the power grid requires the system to be fully loaded or the electricity price is at a high level, the system will actively enter the highest output mode, and the seawater desalination process will enter the lowest power consumption mode;
  • the following process links are realized.
  • the boiler provides heat for the first-stage supercritical CO2 Brayton cycle through the CO2 heater, and provides heat for the second-stage supercritical CO2 Brayton cycle through the CO2 preheater.
  • 2 Brayton cycle combined operation shares a secondary regenerator and realizes the flow distribution of the two Brayton cycles through the first three-way valve and the second three-way valve; the heat source used in the seawater desalination process comes from the low-grade heat source that cannot be used by the thermodynamic cycle.
  • One part of the heat source is transferred to the seawater by the CO2 cooler and the seawater preheater; the other part is the flue gas discharged from the boiler through the seawater heater to further increase the seawater temperature.
  • the steam generators are the primary flasher and the middle flasher; In this working mode, the output of the thermal power system can be adjusted within a reasonable range through the boiler, the heat storage tank and the CO 2 circulating flow;
  • the power grid requires the system to reduce the output or the electricity price is at a high level, the system actively enters the higher output mode, and the seawater desalination process enters the mid-range power consumption mode.
  • the following process links are realized by adjusting the actuators such as valves, pumps and existing pipelines through the control system.
  • the boiler CO 2 heater provides heat for the first-stage supercritical CO 2 Brayton cycle, and the second-stage supercritical CO 2 Brayton cycle
  • the thermal cycle is bypassed; the heat source used in the seawater desalination process comes from the low-grade heat source that cannot be used by the thermodynamic cycle, and part of it is transferred to the seawater by the CO2 cooler and seawater preheater; the other part is the flue gas discharged from the boiler through the seawater heater.
  • the water vapor generating devices are the primary flasher, the middle flasher, and the final flasher, and the fan in the final flasher is in a normally closed state;
  • the tank and CO 2 circulating flow adjust the output of the thermodynamic system within a reasonable range, and at the same time appropriately increase the seawater flow to improve the fresh water production;
  • the power grid requires the system to continue to reduce the output or the electricity price is in the middle, the system actively enters the lower output mode, and the seawater desalination process enters the mid-range power consumption mode.
  • the pipeline realizes the following process links.
  • the boiler provides heat for the first-stage supercritical CO2 Brayton cycle through the CO2 heater, and the second-stage supercritical CO2 Brayton cycle is bypassed.
  • the regenerator is bypassed; the heat source used in the seawater desalination process comes from the low-grade heat source that cannot be used by the thermodynamic cycle, and part of it is transferred to the seawater by the CO2 cooler and seawater preheater; the other part is the flue gas discharged from the boiler through the seawater heater
  • the water vapor generating devices are the primary flasher, the middle flasher, and the final flasher, and the fan in the final flasher is in a normally closed state;
  • the tank and CO 2 circulating flow adjust the output of the thermodynamic system within a reasonable range, and at the same time appropriately increase the seawater flow to improve the fresh water production;
  • the power grid requires the system to have low-load output or the electricity price is at a low level, the system will actively enter the lowest output mode, and the seawater desalination process will enter the highest power consumption mode;
  • the boiler provides heat for the secondary supercritical CO2 Brayton cycle through the CO2 preheater, the original system is reconstructed into a secondary supercritical CO2 Brayton cycle superimposed CO2 cooling cycle, and the primary supercritical CO2
  • the Brayton cycle is bypassed;
  • the heat source used in the seawater desalination process comes from the low-grade heat source that cannot be used by the thermodynamic cycle, part of which is transferred to seawater by the CO2 cooler and seawater preheater; the other part is the flue gas discharged from the boiler is heated by seawater
  • the water vapor generators are the primary flasher, the middle flasher, and the final flasher, and the fan in the final flasher is always on; in this working mode, the boiler, storage
  • the thermal tank and CO 2 circulating flow adjust the output
  • the supercritical CO2 Brayton cycle of the present invention is different from the traditional regenerative cycle, reheating cycle, recompression cycle and intercooling, etc.
  • the improvement of the traditional supercritical CO2 Brayton cycle is in a low pressure state
  • the lower shunt flows together under high pressure
  • the supercritical CO Brayton cycle of the present invention splits under low pressure and merges under low pressure, and generates a third-stage pressure in addition to the high and low pressures of traditional operation and can be within a certain range. Adjustment can make full use of the adjustability of CO 2 compression equipment and expansion equipment to greatly improve the output flexibility of the system.
  • the seawater desalination system of the present invention is improved on the traditional multi-stage flash evaporation system.
  • the primary flasher and the middle flasher are filled with pebbles to increase the speed of water vapor generation.
  • the final flasher is combined with air conditioning cooling tower technology. Increase energy consumption by combining water distributors, grills and fans to increase the rate of water vapor generation in the low temperature section.
  • the present invention fully exploits the advantages of small size and strong adjustability of CO 2 compression and expansion equipment, supplemented by an adjustable seawater desalination system, which can not only realize a large-scale adjustment of the thermal power generation system, but also provide the The excess heat and the heat that the system itself cannot use provide a continuously variable heat load, which further improves the economic benefits of thermal power generation, and can also be applied to other brackish water desalination scenarios in addition to seawater desalination.
  • the first adaptation scenario of the working condition mode of the present invention is that when the power grid requires the power station to operate at full load or the electricity price is the highest, the first and second stage supercritical CO 2 Brayton cycles are combined to operate, and the seawater desalination system operates with minimum power consumption , to meet the requirements of power grid fluctuations or to achieve maximum economic benefits.
  • Working condition mode 2 of the present invention adapts to the scenario that when the power grid requires the power station to further reduce the output or the electricity price is at a higher level, the system actively enters the higher output mode, and the first-stage supercritical CO 2 Brayton cycle independently operates the seawater desalination process Enter into mid-range power consumption operation to meet the requirements of grid fluctuations or to achieve maximum economic benefits.
  • the third adaptation scenario of the present invention is that when the power grid requires the power station to continue to reduce the output or the electricity price is in the middle, the system actively enters the lower output mode, the first-stage supercritical CO 2 Brayton cycle operates independently and the second-stage loop is removed.
  • the thermal process seawater desalination process enters the mid-range power consumption operation to meet the requirements of power grid fluctuations or to achieve maximum economic benefits.
  • the present invention is in working condition mode 4. This mode adapts to the scenario that when the power grid requires low-load output of the power station or the electricity price is at a low level, the system actively enters the lowest output mode, and the secondary supercritical CO 2 Brayton cycle superimposes the CO 2 cooling cycle operation. The desalination process enters the highest power consumption mode to meet the requirements of grid fluctuations or to achieve maximum economic benefits.
  • Fig. 1 The power cycle of supercritical carbon dioxide combined with seawater desalination is a highly flexible electricity and water combined production system of the present invention.
  • FIG. 2 is a schematic diagram of a working mode of a combined electricity and water production system according to an embodiment of the present invention.
  • FIG. 3 is a schematic diagram of the second working mode of the electricity and water combined production system according to the embodiment of the present invention.
  • FIG. 4 is a schematic diagram of the third working mode of the electricity and water combined production system according to the embodiment of the present invention.
  • FIG. 5 is a schematic diagram of four working modes of a combined electricity and water production system according to an embodiment of the present invention.
  • FIG. 6 is a schematic diagram of the first state of the heat source combined with the heat storage system of the present invention.
  • FIG. 7 is a schematic diagram of the second state of the heat source combined with the heat storage system of the present invention.
  • Figure 8 is a schematic structural diagram of the primary flash evaporator of the present invention.
  • Figure 9 is a schematic structural diagram of the middle-stage flash evaporator of the present invention.
  • Figure 10 is a structural view of the final stage flasher of the present invention.
  • Figure 11 is a perspective view of the structure of the final stage flasher of the present invention.
  • Figure 12 is a schematic diagram of the fresh water storage tank of the present invention.
  • a highly flexible electricity and water co-production system based on supercritical carbon dioxide power cycle combined with seawater desalination consisting of boiler 7, heat storage tank 8, CO2 heater 3a, CO2 preheater 3b , seawater heater 6a, first working fluid pump 11a, second intermediate working fluid pump 11b equipment composed of heat source circulation system; by CO2 heater 3a, CO2 preheater 3b, primary expander 1a, secondary expansion
  • a thermodynamic cycle system composed of equipment 1b, primary compressor 2a, secondary compressor 2b, primary regenerator 4a, secondary regenerator 4b and CO2 cooler 5; composed of CO2 cooler 5, seawater Heater 6a, seawater preheater 6b, steam condenser 6c, primary flasher 12, middle flasher 13, final flasher 14, freshwater storage tank 15, freshwater pump 11c, first seawater pump 11d, second seawater pump 11e, a seawater desalination system composed of equipment such as the third seawater pump 11f, the fourth seawater pump 11g, etc.; the first three-
  • the boiler 7 provides heat for the power cycle through the CO 2 heater 3a and the CO 2 preheater 3b, and a heat storage tank 8 is connected in parallel with the heating cycle pipeline, and is controlled by the second intermediate working fluid pump 11b, the first The second bypass valve 10o, the twelfth three-way valve and the thirteenth three-way valve realize the coordination of heat storage and heat extraction during the system adjustment process;
  • the power cycle passes through the CO 2 heater 3a and the CO 2 preheater 3b absorbs heat from the heat source, and realizes thermoelectric conversion through supercritical CO2 Brayton cycle, and passes through the first three-way valve 10a, the second three-way valve 10b, the third three-way valve 10c, the fourth three-way valve 10d, the third three-way valve 10d, the third three-way valve
  • the waste heat released by the power cycle and the waste heat of boiler flue gas transmitted by the seawater heater 6a, and the low-temperature seawater further improves the energy utilization efficiency by recovering the condensation heat in the flash device.
  • the number of middle-stage flashers 13 can be increased or decreased according to the load requirements.
  • the final-stage final-stage flasher 14 includes a fan 42 to actively increase the evaporation speed, so the matching seawater desalination
  • the heat source outlet of the boiler 7 is connected to the high temperature side inlet of the CO2 heater 3a, the high temperature side outlet of the CO2 heater 3a is connected to the high temperature side inlet of the CO2 preheater 3b, and the high temperature side outlet of the CO2 preheater 3b is connected.
  • the heat source inlet is completed to provide heat to the entire power cycle; at this time, the CO2 heater 3a provides heat for the first-stage supercritical CO2 Brayton cycle, and the CO2 preheater 3b provides the second-stage supercritical CO2 Brayton cycle.
  • the circulating medium CO2 of the first-stage supercritical CO2 Brayton cycle enters the first-stage expander from the low-temperature side outlet of the CO2 heater 3a after being heated in the low-temperature side inlet of the CO2 heater 3a 1a is imported and expanded in its interior and output power, then enters the high-temperature side inlet of the first-stage regenerator 4a from the outlet of the first-stage expander 1a and releases excess heat, and then enters the first-stage regenerator 4a from the high-temperature side outlet of the first-stage regenerator 4a.
  • the outlet of the first three-way valve 10a enters the high-temperature side inlet of the secondary regenerator 4b and is released inside
  • the outlet from the high temperature side of the secondary regenerator 4b enters the inlet of the second three-way valve 10b and is divided into one stream for secondary supercritical CO 2 Brayton cycle and the other stream continues for primary supercritical CO 2 .
  • the high temperature side outlet of the CO2 cooler 5 enters the inlet of the first-stage compressor 2a and is pressurized by the outside world, and is released by a
  • the outlet of the first stage compressor 2a enters the inlet of the low temperature side of the secondary regenerator 4b and recovers the heat of the high temperature side, and then enters the inlet of the low temperature side of the primary regenerator 4a from the outlet of the low temperature side of the secondary regenerator 4b and recovers the high temperature side inside.
  • the first-stage supercritical CO2 Brayton cycle is completed from the low-temperature side outlet of the primary regenerator 4a into the low-temperature side inlet of the CO2 heater 3a ; the circulating medium CO2 of the secondary supercritical CO2 Brayton cycle is in the second stage.
  • the rest of the fluid divided into the three-way valve 10b except entering the first-stage supercritical CO2 Brayton cycle enters the inlet of the second-stage compressor 2b and is pressurized by the outside world, and then enters the CO2 from the outlet of the second-stage compressor 2b 2.
  • the inlet of the low temperature side of the preheater 3b and being heated in it After the inlet of the low temperature side of the preheater 3b and being heated in it, it enters the inlet of the secondary expander 1b from the outlet of the low temperature side of the CO 2 preheater 3b. After it expands inside and outputs work, it enters from the outlet of the secondary expander 1b.
  • the outlet of the first three-way valve 10a enters the high temperature side inlet of the secondary regenerator 4b and is released inside
  • the high temperature side outlet of the secondary regenerator 4b enters the inlet of the second three-way valve 10b and is divided into One stream carries out the first-stage supercritical CO2 Brayton cycle, and the other continues to carry out the second-stage supercritical CO2 Brayton cycle, and enters the inlet of the second-stage compressor 2b to complete the second-stage supercritical CO2 Brayton cycle
  • the heat source used in the seawater desalination process From the low-grade heat source that cannot be used by the thermodynamic cycle, the softened water is boosted by the fresh water pump 11c from the outlet of the water pump 11c into the low-temperature side inlet of the CO2 cooler 5, and after absorbing the cooling heat discharged by the power cycle in its interior, it is cooled by CO2 After the outlet of
  • the outlet 35b of the low temperature condenser 33 in the middle stage flasher 13 enters the primary flasher 12.
  • the outlet 25b of the low-temperature condenser 23 in the middle-stage flasher 13 enters the inlet of the first seawater pump 11d to increase the pressure, and the first seawater pump
  • the outlet of 11d enters (excess seawater is discharged after being diverted by the fourteenth three-way valve 10p) the inlet of the low temperature side of the seawater preheater 6b and after absorbing the cooling heat discharged from the power cycle inside, the seawater enters the seawater from the outlet of the low temperature side of the seawater preheater 6b
  • the outlet from the low temperature side of the seawater heater 6a enters the inlet 25e of the seawater tank 24 of the primary flasher 12 and flashes inside the concentrated seawater from the primary flasher 6a.
  • the outlet 25f at the bottom of the seawater tank 24 of the evaporator 12 enters the inlet of the second seawater pump 11e and increases the pressure inside it, and then enters the inlet 35e of the seawater tank 34 of the middle-stage flasher 13 from the outlet of the second seawater pump 11e and flashes inside the seawater to concentrate the seawater From the bottom outlet 35f of the seawater tank 34 of the middle-stage flasher 13, it enters the fourth seawater pump 11g and is discharged, wherein the flash steam in the primary flasher 12 contacts the fresh water condensed by the low temperature condenser 23 in the primary flasher 12 and passes through the primary flasher 12.
  • the condensed water pan 23 After the condensed water pan 23 is collected, it enters the fresh water storage tank 15 through the outlet 25d of the condensed water pan 23, and the uncondensed part of the flash steam in the primary flasher 12 enters the steam inlet of the middle-stage flasher 13 from the steam outlet 25c of the primary flasher 12 and interacts with it in it.
  • the flash steam in the middle-stage flasher 13 After the flash steam in the middle-stage flasher 13 is mixed, the fresh water condensed by the steam contacting the low-temperature condenser 33 in the middle-stage flasher 13 is collected by the condensate pan 33 in the middle-stage flasher 13 and then enters the fresh water from the outlet 35d of the condensate pan 33.
  • the uncondensed part of the steam in the middle-stage evaporator 13 enters the high-temperature side inlet of the steam condenser 6c from the steam outlet 35c of the middle-stage flasher 13 and releases heat inside it After condensation, the condensed fresh water enters the fresh water storage tank 15 from the high temperature side outlet of the steam condenser 6c; in this working mode, the output of the thermodynamic system can be adjusted within a reasonable range through the boiler 7, the heat storage tank 8 and the circulating flow of CO2 .
  • the power grid requires the system to reduce the output or the electricity price is at a higher level.
  • the system actively enters the higher output mode, and the seawater desalination process enters the mid-range power consumption mode. According to the above, the following process steps are realized by adjusting the actuators such as valves and pumps and the existing pipelines by the controller 9.
  • the heat source outlet of the boiler 7 is connected to the inlet of the high temperature side of the CO2 heater 3a, and the outlet of the high temperature side of the CO2 heater 3a is connected to To the heat source inlet of boiler 7 (the high temperature side of CO 2 preheater 3b is directly bypassed by adjusting the eleventh three-way valve and the twelfth three-way valve of the valve group) to complete the supply of heat to the entire power cycle; at this time, CO 2
  • the heater 3a provides heat for the first-stage supercritical CO2 Brayton cycle, and the second-stage supercritical CO2 Brayton cycle is bypassed; wherein, the circulating medium CO2 of the first-stage supercritical CO2 Brayton cycle passes through the CO2 heater 3a Low temperature side inlet and after being heated inside, from the low temperature side outlet of CO2 heater 3a enters the first stage expander 1a inlet and expands inside it and outputs work, then enters the first stage recuperation from the first stage expander 1a outlet After the inlet of the high temperature side
  • the high temperature side outlet of CO2 cooler 5 enters the inlet of the first-stage compressor 2a and is pressurized by the outside world, and then the first-stage compressor 2a is pressurized by the outside world.
  • the outlet of the compressor 2a enters the low temperature side inlet of the secondary regenerator 4b and recovers the heat on the high temperature side, and then enters the low temperature side inlet of the primary regenerator 4a from the low temperature side outlet of the secondary regenerator 4b and recovers the heat on the high temperature side.
  • the low temperature side outlet of the primary regenerator 4a enters the low temperature side inlet of the CO2 heater 3a to complete the primary supercritical CO2 Brayton cycle;
  • the water is boosted by the fresh water pump 11c and enters the low temperature side inlet of the CO2 cooler 5 from the outlet of the water pump 11c and absorbs the cooling heat discharged from the power cycle inside, and then enters the high temperature side of the seawater preheater 6b from the low temperature side outlet of the CO2 cooler 5
  • the outlet of the high temperature side of the seawater preheater 6b enters the inlet of the fresh water pump 11c to complete the cycle;
  • the flue gas discharged from the boiler 7 is imported from the high temperature side of the seawater heater 6a and releases heat inside it to heat the seawater.
  • the original low-temperature seawater passes through the low-temperature side inlet of the steam condenser 6c and recovers the condensation heat of the water vapor inside, and then enters the low-temperature side of the middle-stage flasher 13 from the low-temperature side outlet of the steam condenser 6c.
  • the outlet 35b of the low temperature condenser 33 in the intermediate flasher 13 enters the inlet 25a of the low temperature condenser 23 in the primary flasher 12 and the water vapor is recovered inside it
  • the outlet 25b of the low-temperature condenser 23 in the middle-stage flasher 13 enters the inlet of the first seawater pump 11d to increase the pressure, and then enters from the outlet of the first seawater pump 11d (excess seawater passes through the fourteenth three-way valve).
  • 10p is discharged after splitting) seawater preheater 6b low temperature side inlet and After absorbing the cooling heat discharged from the power cycle, it enters the low temperature side inlet of the seawater heater 6a from the low temperature side outlet of the seawater preheater 6b and absorbs the waste heat of the flue gas of the boiler 7 inside it, and then enters from the low temperature side outlet of the seawater heater 6a.
  • the concentrated seawater After the inlet 25e of the seawater tank 24 of the primary flasher 12 is flashed inside the concentrated seawater, the concentrated seawater enters the inlet of the second seawater pump 11e from the bottom outlet 25f of the seawater tank 24 of the primary flasher 12 and is boosted in its interior, and then the concentrated seawater is pumped by the second seawater pump.
  • the concentrated seawater enters the inlet of the third seawater pump 11f from the outlet 35f at the bottom of the seawater tank 34 of the middle-stage flasher 13 and is boosted inside it, and then is pumped by the third seawater pump 11f.
  • the outlet of the three seawater pumps 11f enters the inlet 46a of the water distributor 43 of the final flasher 14, and the seawater further concentrated through the grid 44 of the water distributor 43 is collected to the seawater tank 45 of the final flasher 14 and enters the fourth seawater pump 11g from the bottom thereof for discharge.
  • the fresh water condensed by the flash steam in the primary flasher 12 contacting the low-temperature condenser 23 in the primary flasher 12 is collected by the condensate pan 23 in the primary flasher 12 and then enters the fresh water storage tank 15 from the outlet 25d of the condensate pan 23 , the uncondensed part of the steam in the primary flasher 12 enters the steam inlet of the middle-stage flasher 13 from the steam outlet 25c of the primary flasher 12 and is mixed with the flashed steam in the middle-stage flasher 13, and the steam contacts the middle-stage flasher 13.
  • the fresh water condensed by the low temperature condenser 33 is collected by the condensate pan 33 in the middle-stage flasher 13 and then enters the fresh water storage tank 15 from the outlet 35d of the condensate pan 33, and the uncondensed part of the steam in the middle-stage flasher 13 passes through the fifteenth three-way valve.
  • the outlet of the fifteenth three-way valve 10q enters the inlet of the high temperature side of the steam condenser 6c and releases heat and condenses inside, and the condensed fresh water is released by the high temperature of the steam condenser 6c.
  • the side outlet enters the fresh water storage tank 15 .
  • the output of the thermodynamic system can be adjusted within a reasonable range through the boiler 7, the heat storage tank 8 and the circulating flow of CO 2 , and at the same time, the flow of seawater can be appropriately increased to increase the fresh water production.
  • the power grid requires the system to further reduce the output or the electricity price is in the middle.
  • the system actively enters the mid-range output mode, and the seawater desalination process enters the mid-range power consumption mode. According to the above, the following process steps are realized by adjusting the actuators such as valves and pumps and the existing pipelines by the controller 9.
  • the heat source outlet of the boiler 7 is connected to the inlet of the high temperature side of the CO2 heater 3a, and the outlet of the high temperature side of the CO2 heater 3a is connected to To the heat source inlet of boiler 7 (the high temperature side of CO 2 preheater 3b is directly bypassed by adjusting the eleventh three-way valve and the twelfth three-way valve of the valve group) to complete the supply of heat to the entire power cycle; at this time, CO 2
  • the heater 3a provides heat for the first-stage supercritical CO2 Brayton cycle, and the second-stage supercritical CO2 Brayton cycle is bypassed; wherein, the circulating medium CO2 of the first-stage supercritical CO2 Brayton cycle passes through the CO2 heater 3a Low temperature side inlet and after being heated inside, from the low temperature side outlet of CO2 heater 3a enters the first stage expander 1a inlet and expands inside it and outputs work, then enters the first stage recuperation from the first stage expander 1a outlet After the inlet of the high temperature side
  • the outlet of the first-stage compressor 2a enters the low-temperature side inlet of the first-stage regenerator 4a (through the linkage of the third three-way valve 10c and the fourth three-way valve 10d of the valve group, the second-stage heat recovery is directly bypassed.
  • the low-temperature side outlet of the primary regenerator 4a enters the low-temperature side inlet of the CO2 heater 3a to complete the first-stage supercritical CO2 Brayton cycle;
  • the heat source used in the seawater desalination process From the low-grade heat source that cannot be used by the thermodynamic cycle, the softened water is boosted by the fresh water pump 11c from the outlet of the water pump 11c into the low-temperature side inlet of the CO2 cooler 5, and after absorbing the cooling heat discharged by the power cycle in its interior, it is cooled by CO2
  • the outlet of the low temperature side of the boiler 5 enters the inlet of the high temperature side of the seawater preheater 6b and transfers heat to the seawater
  • the outlet of the high temperature side of the seawater preheater 6b enters the inlet of the fresh water pump 11c to complete the cycle;
  • the flue gas discharged from the boiler 7 is heated by the sea
  • the outlet 35b of the low temperature condenser 33 in the middle stage flasher 13 enters the primary flasher 12.
  • the outlet 25b of the low-temperature condenser 23 in the middle-stage flasher 13 enters the inlet of the first seawater pump 11d to increase the pressure, and the first seawater pump 11d outlet enters (excess seawater is shunted by the fourteenth three-way valve 10p and then discharged).
  • the low temperature side outlet of the seawater preheater 6b absorbs the cooling heat discharged from the power cycle, the low temperature side outlet of the seawater preheater 6b enters the low temperature side inlet of the seawater heater 6a and absorbs the flue gas of the boiler 7 inside it.
  • the waste heat After the waste heat, it enters the inlet 25e of the first seawater tank 24 of the primary flasher 12 from the low temperature side outlet of the seawater heater 6a and is flashed inside the concentrated seawater from the outlet 25f of the bottom of the first seawater tank 24 of the primary flasher 12.
  • the outlet of the second seawater pump 11e After the inlet of the second seawater pump 11e increases the pressure inside the second seawater pump 11e, the outlet of the second seawater pump 11e enters the inlet 35e of the second seawater tank 34 of the middle-stage flasher 13 and flashes inside the concentrated seawater.
  • the seawater further concentrated by the grid 44 is collected into the third seawater tank 45 of the final flasher 14 and discharged from the bottom into the fourth seawater pump 11g, wherein the flash steam in the primary flasher 12 contacts the low temperature condenser 23 in the primary flasher 12
  • the condensed fresh water is collected by the condensate pan 23 in the primary flasher 12 and then enters the fresh water storage tank 15 from the outlet 25d of the condensate pan 23, and the uncondensed part of the steam in the primary flasher 12 enters the intermediate flash from the steam outlet 25c of the primary flasher 12.
  • the fresh water condensed by the steam contacting the low-temperature condenser 33 in the middle-stage flasher 13 is collected by the condensed water pan 33 in the middle-stage flasher 13.
  • the fresh water storage tank 15 enters the fresh water storage tank 15 from the outlet 35d of the condensate pan 33, and the uncondensed part of the steam in the middle-stage flasher 13 is mixed with the flash steam in the final-stage flasher 14 through the inlet of the fifteenth three-way valve 10q.
  • the outlet of the through valve 10q enters the inlet of the high temperature side of the steam condenser 6c and after the heat is released and condensed inside, the condensed fresh water enters the fresh water storage tank 15 from the outlet of the high temperature side of the steam condenser 6c.
  • the output of the thermodynamic system can be adjusted within a reasonable range through the boiler 7, the heat storage tank 8 and the circulating flow of CO 2 , and at the same time, the flow of seawater can be appropriately increased to increase the fresh water production.
  • the power grid requires the system to have low-load output or the electricity price is at a low level.
  • the system actively enters the lowest output mode, and the seawater desalination process enters the highest power consumption mode; The following process steps are realized.
  • the heat source outlet of the boiler 7 is connected to the high temperature side inlet of the CO 2 preheater 3b (by adjusting the eighth three-way valve 10i and the ninth three-way valve 10j of the valve group, the high temperature side of the CO 2 heater 3a is directly bypassed.
  • the high temperature side outlet of the CO 2 preheater 3b is connected to the heat source inlet of the boiler 7 to provide heat for the entire power cycle; at this time, the CO 2 preheater 3b provides heat for the secondary supercritical CO 2 Brayton cycle, and the primary supercritical The CO 2 Brayton cycle is bypassed; wherein, the circulating medium CO 2 of the secondary supercritical CO 2 Brayton cycle passes through the low temperature side inlet of the CO 2 preheater 3b and is heated inside it, and then is heated by the CO 2 preheater 3b The outlet of the low temperature side enters the inlet of the secondary expander 1b, expands inside it and outputs power, and then enters the inlet of the high temperature side of the secondary regenerator 4b from the outlet of the secondary expander 1b, and releases excess heat in it, and then the outlet of the secondary expander 1b enters the inlet of the high temperature side of the secondary regenerator 4b.
  • the outlet of the high temperature side of the heater 4b enters the inlet of the secondary compressor 2b and is pressurized by the outside to complete the secondary supercritical CO2 Brayton cycle, and establish a CO2 cooling cycle in which the CO2 fluid enters the secondary recuperation
  • the inlet of the low temperature side of the CO2 cooler 4b absorbs the heat of the high temperature side in it, it enters the inlet of the high temperature side of the CO2 cooler 5 from the outlet of the low temperature side of the secondary regenerator 4b and releases the excess heat, and the high temperature side of the CO2 cooler 5
  • the outlet of the primary compressor 2a enters the low temperature side inlet of the secondary regenerator 4b to complete the CO2 cooling cycle (by adjusting the valve group first.
  • the three-way valve 10a, the second three-way valve 10b, the third three-way valve 10c, the fourth three-way valve 10d and the fifth three-way valve 10e are linked to make the CO2 heater 3a, the primary regenerator 4a and the primary expansion Machine 1a is bypassed and the system is reconstructed into a secondary supercritical CO2 Brayton cycle superimposed with CO2 cooling cycle);
  • the heat source used in the seawater desalination process comes from a low-grade heat source that cannot be used by the thermodynamic cycle, and the softened water is boosted by the freshwater pump 11c
  • the low temperature side outlet of CO2 cooler 5 enters the high temperature side inlet of seawater preheater 6b and transferring the heat inside it
  • the high temperature side outlet of the seawater preheater 6b enters the inlet of the fresh water pump 11c to complete the cycle;
  • the original low temperature seawater passes through the low temperature side inlet of the steam condenser 6c and recovers the condensation heat of the water vapor inside it, and then enters the low temperature condenser 33 inlet 35a of the intermediate flasher 13 from the low temperature side outlet of the steam condenser 6c and is stored in the low temperature condenser 33.
  • the outlet 35b of the low-temperature condenser 33 enters the inlet 25a of the low-temperature condenser 23 in the primary flasher 12, and after the condensation heat of the water vapor is recovered inside, the outlet 25b of the low-temperature condenser 23 in the middle-stage flasher 13 enters the first seawater pump 11d After the pressure is raised in the inlet, it enters from the outlet of the first seawater pump 11d (excess seawater is diverted by the fourteenth three-way valve 10p and then discharged) The inlet of the low temperature side of the seawater preheater 6b absorbs the cooling heat discharged by the power cycle inside it.
  • the concentrated seawater enters the inlet of the second seawater pump 11e from the outlet 25f at the bottom of the first seawater tank 24 of the primary flasher 12, and after its internal pressure is increased, the concentrated seawater enters from the outlet of the second seawater pump 11e.
  • the concentrated seawater After the inlet 35e of the third seawater tank 34 of the middle-stage flasher 13 is flashed inside the concentrated seawater, the concentrated seawater enters the inlet of the third seawater pump 11f from the bottom outlet 35f of the third seawater tank 34 of the middle-stage flasher 13 and is pressurized inside.
  • the fourth seawater pump 11g is discharged, wherein the fresh water condensed by the flash steam in the primary flasher 12 contacting the low temperature condenser 23 in the primary flasher 12 is collected by the condensate pan 23 in the primary flasher 12 and then exits from the condensate pan 23 25d enters the fresh water storage tank 15, and the uncondensed part of the steam in the primary flasher 12 enters the steam inlet of the middle-stage flasher 13 from the steam outlet 25c of the primary flasher 12 and mixes with the flash steam in the middle-stage flasher 13, and the steam contacts.
  • the fresh water condensed by the low-temperature condenser 33 in the middle-stage flasher 13 is collected by the condensed water pan 33 in the middle-stage flasher 13 and then enters the fresh water storage tank 15 from the outlet 35d of the condensed water pan 33, and the uncondensed part of the steam in the middle-stage flasher 13 passes through.
  • the outlet of the fifteenth three-way valve 10q enters the high temperature side inlet of the steam condenser 6c and releases heat and condenses inside, and condenses the fresh water. It enters the fresh water storage tank 15 from the high temperature side outlet of the steam condenser 6c.
  • the output of the thermodynamic system can be adjusted within a reasonable range through the boiler 7, the heat storage tank 8 and the circulating flow of CO 2 , and at the same time, the flow of seawater can be appropriately increased to improve the fresh water production.
  • the fan in the final flasher 14 42 is always open.
  • the heat storage tank 8 has three operating conditions, the heat storage condition, the heat-up condition and the shutdown condition.
  • the intermediate working medium is heated in the boiler 7 and enters the sixth through the inlet of the boiler 7.
  • the main part is used for heating the thermodynamic cycle, and the excess part enters the inlet of the intermediate working fluid pump 11b and boosts the pressure inside it, and then enters the inlet of the heat storage tank 8 from the outlet of the intermediate working fluid pump 11b and enters the inlet of the heat storage tank 8 inside it.
  • the heat After the heat is released, it enters the seventh three-way valve from the outlet of the heat storage tank for 10h and returns to the boiler 7 after mixing with the fluid that has completed the heating thermodynamic cycle; A part of the outflow of the three-way valve 10h flows into the inlet of the boiler 7 and absorbs heat in it, and then enters the sixth three-way valve 10g from the outlet of the boiler 7, and the other part flows into the inlet of the heat storage tank 8 and absorbs heat in it, and then the heat is absorbed by the heat storage tank 8.
  • the outlet of tank 8 enters the sixth three-way valve 10g (by adjusting the twelfth three-way valve 10m, the thirteenth three-way valve 10n and the second bypass valve 10o to bypass the intermediate working fluid pump 11b), two fluids After the sixth three-way valve 10g converges, the thermodynamic cycle is heated; under the closed condition, the sixth three-way valve 10g and the seventh three-way valve 10h of the valve group are adjusted to bypass the intermediate working fluid pump 11b and the heat storage tank 8.
  • the heat storage tank 8 When the high flexibility electricity and water combined production system based on supercritical carbon dioxide power cycle combined with seawater desalination operates stably in working mode 1, working mode 2, working mode 3 and working mode 4, the heat storage tank 8 is in the closed condition, When the system switches from the high power output mode to the low power output mode (such as switching from the working mode to the working mode 2) or in a specific working mode, the system adjusts the flow to reduce the power output and the boiler cannot quickly reduce the heat output when the heat storage tank 8 is in the storage tank 8. In thermal condition, the heat storage tank 8 is in thermal storage condition when the system switches from low power output mode to high power output mode or when the system adjusts the flow in a specific working mode to increase the power output but the boiler cannot rapidly increase the heat output.
  • the primary flasher 12 is composed of five parts: a first shell 21, a first low temperature condenser 22, a first condensate pan 23, a first seawater tank 24, and a second seawater pump 11e.
  • the primary flasher 12 includes six interfaces: a first low temperature seawater inlet 25a, a first low temperature seawater outlet 25b, a first steam outlet 25c, a first fresh water outlet 25d, a first high temperature seawater inlet 25e and a first high temperature seawater outlet 25f, wherein Cobblestones are stacked in the first seawater tank 24 to increase the air outlet speed, and a first fresh water outlet 25d is drawn from the bottom of the first condensate pan 23 to discharge condensate water;
  • the water vapor flashed in the primary flasher 12 contacts the first low temperature condenser 22 in the primary flasher 12 and condenses into fresh water, which is collected by the first condensate pan 23 in the primary flasher 12 for final convergence.
  • the remaining steam flows into the middle-stage flasher 13 and mixes with the water vapor flashed out of the middle-stage flasher 13, contacts with the low-temperature condenser 32 in the middle-stage flasher 13 and condenses into fresh water, which is mixed with the middle-stage flasher 13.
  • the second condensed water pan 33 in the middle is collected and finally converged to the fresh water storage tank 15, and the remaining steam is mixed with the steam from the expansion and flashing in the final stage flasher 14 through the fifteenth three-way valve 10q and enters the high temperature side of the steam condenser 6c.
  • the thermal condensation finally flows into the fresh water storage tank 15;
  • the middle-stage flasher 13 is composed of five parts: a second shell 31, a second low-temperature condenser 32, a second condensate pan 33, a second seawater tank 34, and a third seawater pump 11f.
  • the middle-stage flasher 13 is composed of five parts. 13 includes six interfaces of a second low-temperature seawater inlet 35a, a second low-temperature seawater outlet 35b, a second water vapor outlet 35c, a second freshwater outlet 35d, a second high-temperature seawater inlet 35e and a second high-temperature seawater outlet 35f, wherein the first Cobblestones are stacked in the second seawater tank 34 to increase the gas outlet speed.
  • the bottom of the second condensate pan 33 leads out a second fresh water outlet 35d for discharging condensed water.
  • the difference from the primary flasher 12 is that the middle flasher 13 can meet the needs of the seawater desalination process.
  • the second seawater tank 34 in the middle flasher 13 can be equipped with a flue gas waste heat recovery device according to the needs of the seawater desalination process to utilize the flue gas discharged from the high temperature side of the seawater heater 6a.
  • the final flasher 14 is composed of a third casing 41, a fan 42, a water distributor 43, a grill 44, a third seawater tank 45, and a third seawater pump 11f.
  • the fan 42 It is used to increase the disturbance to improve the evaporation rate of seawater on the surface of the grid 44 .
  • the fresh water storage tank 15 adopts a sealed cabin 51, and the upper part is equipped with an exhaust valve 52 for regular vacuuming to provide negative pressure for the fresh water side of the seawater desalination process;
  • the number of the middle-stage flashers 13 can be increased or decreased correspondingly according to the evaporation amount required by the process.
  • the fifteenth three-way valve 10q, the sixteenth three-way valve 10r, and the seventeenth three-way valve 10s are used to bypass the final stage flasher. 14.

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Abstract

一种基于超临界二氧化碳动力循环结合海水淡化的动力电站，通过超临界二氧化碳动力循环结合海水淡化的一体化工艺，该系统采用新型双级超临界CO2布雷顿循环来降低热源排气温度，提升循环热效率，从而达到热动力电站输出灵活性、可调性之目的；相对应的加强低温、动态热源在海水淡化工艺的利用效能，使之成为动力电站的常备"柔性负载"，进一步提升系统整体效能和灵活性。还提供了一种该电站的运行方法。

Description

一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站及其调节方法 技术领域
本发明属于热能动力及海水淡化技术领域，涉及一种热能综合利用系统，特别涉及基于超临界二氧化碳(S-CO 2)循环的灵活性热动力系统和基于能量梯级利用的多级海水淡化系统，构成的高灵活性电、水联合生产系统及运行方法。
背景技术
清洁能源高比例并网是外来能源生产与消费的大形势。目前的储能配置规模很低尚无法实现对电力系统全面的调节，需要大量火力电站参与调节。根据各国未来规划各种能源参与比例，高灵活性的热动力电站将作为最基础的调节措施与其他清洁能源长久共存。水蒸气动力循环为充分利用蒸汽能量，所用透平一般采用多级膨胀，尤其是随着膨胀过程蒸汽压力和密度下降叶轮尺寸逐级递增。现阶段高效水蒸气透平可以达到50级以上，尺寸和热惯性巨大不利于调节。为达到调节输出不得不采用低压抽气的手段，牺牲了大量有用能。
相比于传统蒸汽朗肯循环的工质水，CO 2的临界点较低，超临界状态容易实现。在超临界区域，CO 2的热力性能具有多方面优势。传热性能方面：其密度接近液体，传热效率高；在动力性能方面：其黏性接近气体，易于扩散，流动性强，做功能力强。所述S-CO 2性能特征使S-CO 2布雷顿循环可适应更广的温度范围和更高的系统循环效率。此外，S-CO 2布雷顿循环的结构紧凑、体积小，重量轻。在相同发电装机的条件下，其透平尺寸是蒸汽发电系统的1/30。因此，S-CO 2布雷顿循环在快速启动、应急反应和能源利用效率方面都更具优势，尤其若作为调峰电站其运营经济性的优势明显高于蒸汽循环，有望成为下一代高效经济的热动力发电技术。
为了提高S-CO 2布雷顿循环的效率，将回热、再热、分级压缩、中间冷却等热力学过程应用到S-CO 2布雷顿循环中，由此衍生出S-CO 2布雷顿循环的多种改进形式。但目前大多循环结构采用固定形式，由于各个工艺环节关联紧密耦合程度高，对系统调节以流量调节和分流比调节为主。这也造成了系统调节范围受限，不能充分发挥透平的高效性能和灵活性潜力。此外，应动力电站灵活性调节的需要，随着系统吸热量和系统效率变化，系统放热过程也将大范围波动，与之对应有大量的低品位热能产生。热力循环海水淡化工艺是良好的柔性负载，在新型火力电站建设初期进行配合实施可有效提升系统能源效率和经济性。
我国淡水资源严重短缺，人均占有量只有世界平均水平的25％，我国淡水资源分布情况呈现由东南向西北逐渐减少的分布趋势。全国661个城市中有近400个供水不足，其中110个城市严重缺水；百万人口以上特大城市中有30个长期受缺水问题困扰；其中华北地区水资源紧缺已成为制约国民经济发展的重要障碍。另外，在世界范围来看全世界有100多个国家存在着不同程度的缺水，28个被列为严重缺水国家，许多国家都出现了买水度日的情况。海水淡化技术是未来淡水生产的重要途径，主要有多级闪蒸、多效蒸发和反渗透三种技术路线。由于多级闪蒸技术可应用于更低温度段，广泛利用工业工艺难以利用的低品位热， 占据60％以上的淡化市场份额。
目前在热电成产工艺末端加装多级闪蒸的海水淡化装置技术上已较为成熟。为进一步降低热源排气温度，提升高品质热量的利用率，提高热动力电站的灵活输出，简单的在传统热动力循环工艺末端加装海水淡化工艺并不能满足实际需求。一方面需对热动力循环本身的灵活性进行改进，相匹配的海水淡化工艺也应进行一体化设置。如采用新型的S-CO 2动力循环工艺进行发电，锅炉的排气温度会大大降低，因而在海水淡化一侧的循环热效率需要进一步提升以降低海水淡化工艺全生命周期的成本。
发明内容
本发明是基于超临界二氧化碳动力循环结合海水淡化的一体化工艺，来降低热源排气温度，提升热动力循环热效率，提升热动力电站输出的灵活性及可调性；相对应的加强低温、动态热源在海水淡化工艺的利用效能，使之成为动力电站的常备“柔性负载”，进一步提升系统整体效率和灵活性。
为了实现上述的技术特征，本发明的目的是这样实现的：一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，它包括热源循环系统、热动力循环系统、海水淡化系统和控制系统；
所述热源循环系统与热动力循环系统和海水淡化系统系统相连，并分别为其提供工作过程中所需要的热源；
所述控制系统同时与热源循环系统、热动力循环系统和海水淡化系统的各个执行机构相连，并控制其相应工作。
所述热源循环系统包括锅炉、储热罐、CO 2加热器、CO 2预热器、海水加热器、第二旁通阀门、第六三通阀门、第七三通阀门、第八三通阀门、第九三通阀门、第十三通阀门、第十一三通阀门、第十二三通阀门、第十三三通阀门、第一中间工质泵、第二中间工质泵和配套管理；
所述锅炉为系统原始热源，锅炉与CO 2加热器和CO 2预热器串联，并为热动力循环系统提供热量；锅炉与海水加热器相连，并为海水淡化系统提供热量；
所述储热罐并联在CO 2加热器、CO 2预热器构成的串联换热器组两侧，用以调节锅炉换热过程中由于热惰性与负载CO 2加热器、CO 2预热器存在的不匹配问题；
所述第一中间工质泵和第二中间工质泵分别与热动力循环系统和储热罐相连，并分别用于调节加热热动力循环系统和储热罐的流量分配；所述第十二三通阀门、第十三三通阀门和第二旁通阀门和第二中间工质泵并连，并实现储热罐的吸放热以及流量调节；
所述第八三通阀门、第九三通阀门用以旁通CO 2加热器的高温侧、第十三通阀门、第十一三通阀门用以旁通CO 2预热器的高温侧来实现热动力循环的大范围灵活性调控。
所述储热罐储热材料选用熔融盐或液态金属，根据电力系统要求当系统负荷下降，锅炉热量不能快速调节时，将部分热量储存在储热罐，当系统负荷上升，锅炉热量不能快速调节时，则提出储热罐中储存的热量为动力循环补充热量；
所述CO 2加热器、CO 2预热器和海水加热器采用直接内置安装在锅炉内，去掉中间介质直接加热CO 2或海水。
所述热动力循环系统包括CO 2加热器、CO 2预热器、一级膨胀机、二级膨胀机、一级压 缩机、二级压缩机、一级回热器、二级回热器、CO 2冷却器、第一旁通阀门、第一三通阀门、第二三通阀门、第三三通阀门、第四三通阀门、第五三通阀门和配套管路；
所述热动力循环系统采用CO 2为工质，其嵌套了两级超临界CO 2布雷顿循环：包括一级超临界CO 2布雷顿循环和二级超临界CO 2布雷顿循环；CO 2加热器为所述一级超临界CO 2布雷顿循环提供热量，之后通过CO 2预热器为所述二级超临界CO 2布雷顿循环提供热量，量实现了一级、二级超临界CO 2布雷顿循环间接结合与能量的梯级利用。
所述一级超临界CO 2布雷顿循环的循环工质为超临界CO 2，CO 2工质先后流经一级压缩机、二级回热器低温侧、一级回热器低温侧、CO 2加热器低温侧、一级膨胀机、一级回热器高温侧、第一三通阀门、二级回热器高温侧、第二三通阀门、CO 2冷却器高温侧、一级压缩机完成循环，相对应的CO 2流体先后经历了升压、吸热、吸热、吸热、膨胀、放热、汇流、放热、分流、放热、升压几个工艺实现吸热并做工的整体工艺流程；
所述二级超临界CO 2布雷顿循环的循环工质为超临界CO 2，CO 2工质先后流经二级压缩机、CO 2预热器低温侧、二级膨胀机、第一三通阀门、二级回热器高温侧、第二三通阀门、二级压缩机完成循环，相对应的CO 2流体先后经历了升压、吸热、膨胀、汇流、放热、分流、升压几个工艺实现吸热并做工的整体工艺流程；
所述一级、二级超临界CO 2布雷顿循环通过第一三通阀门、第二三通阀门和二级回热器实现上述一级、二级超临界CO 2布雷顿循环的直接相互结合，通过第一三通阀门、第二三通阀门调节二级循环的分流比例来调整系统运行；
所述第一三通阀门、第二三通阀门和第一旁通阀门用于旁通二级超临界CO 2布雷顿循环使一级超临界CO 2布雷顿循环独立运行，所述第三三通阀门、第四三通阀门、第五三通阀门用于旁通一级超临界CO 2布雷顿循环使二级超临界CO 2布雷顿循环独立运行；
一级膨胀机、二级膨胀机、一级压缩机、二级压缩机之间为满足调节工况采用变速器加离合器的链接方式；CO 2加热器、CO 2预热器、一级回热器、二级回热器、CO2冷却器使用印刷电路板换热器。
所述海水淡化系统包括CO 2冷却器、海水加热器、海水预热器、蒸汽冷凝器、初级闪蒸器、中段闪蒸器、末级闪蒸器、淡水储罐、第十四三通阀门、第十五三通阀门、第十六三通阀门、第十七三通阀门、淡水泵、第一海水泵、第二海水泵、第三海水泵、第四海水泵和配套管路；
所述海水加热器、海水预热器、蒸汽冷凝器采用抗腐蚀堵、塞能力较强、对压力要求不高、经济性好的管壳式换热器，换热器内换热管束采用铜管；
加热海水的热量来源于三部分，包括通过蒸汽冷凝器、中段闪蒸器、初级闪蒸器回收海水闪蒸后携带的冷凝热，通过海水预热器回收热动力循环末端冷却的热量，通过海水加热器回收热源循环中烟气废热，其中利用软化水先后流经淡水泵、CO 2冷却器低温侧、海水预热器高温侧、淡水泵，对应完成升压、吸热、放热、升压的循环工艺，将热动力循环末端冷却放出的热量间接传递给海水，其中软化水循环主要是为了保护CO 2冷却器所采用的印刷电路板换热器，或者采用简化系统，简化后直接用一台换热器将动力循环末端的冷却热量直接用于加热海水；
抽取自然的低温海水先后流经蒸汽冷凝器低温侧、中段闪蒸器中的低温冷凝器、初级闪蒸器中的低温冷凝器、第一海水泵、至第十四三通阀门、海水预热器低温侧、海水加 热器低温侧、初级闪蒸器的第一海水槽、第二海水泵11e、中段闪蒸器的第二海水槽、第三海水泵、末级闪蒸器中布水器格栅和第三海水槽、第四海水泵排放完成海水浓缩，相对应的海水流体先后经历了吸热、吸热、吸热、升压、分流、吸热、吸热、闪蒸浓缩、升压、闪蒸浓缩、升压、扩容闪蒸浓缩、升压排放几个工艺实现吸热低压闪蒸浓缩的工艺流程。
所述初级闪蒸器由第一外壳、第一低温冷凝器、第一冷凝水盘、第一海水槽、第二海水泵五个部分组成，所述初级闪蒸器包含第一低温海水进口、第一低温海水出口、第一水蒸气出口、第一淡水出口、第一高温海水进口和第一高温海水出口六个接口，其中所述第一海水槽中堆砌鹅卵石提高出气速度，所述第一冷凝水盘底部引出第一淡水出口用以排出冷凝水；
所述初级闪蒸器中闪蒸出的水蒸气，接触初级闪蒸器中的第一低温冷凝器冷凝成淡水并由初级闪蒸器中的第一冷凝水盘收集最终汇聚至淡水储罐，剩余蒸汽流入中段闪蒸器并与中段闪蒸器中闪蒸出的水蒸气混合，接触与中段闪蒸器中的低温冷凝器冷凝成淡水并由与中段闪蒸器中的第二冷凝水盘收集最终汇聚至淡水储罐，剩余蒸汽通过第十五三通阀门与末级闪蒸器中扩容闪蒸出的水蒸气混合进入蒸汽冷凝器高温侧放热冷凝最终汇入淡水储罐；
所述中段闪蒸器由第二外壳、第二低温冷凝器、第二冷凝水盘、第二海水槽、第三海水泵五个部分组成，所述中段闪蒸器包含第二低温海水进口、第二低温海水出口、第二水蒸气出口、第二淡水出口、第二高温海水进口和第二高温海水出口六个接口，其中所述第二海水槽中堆砌鹅卵石提高出气速度，所述第二冷凝水盘底部引出第二淡水出口用以排出冷凝水，与初级闪蒸器不同的是中段闪蒸器能够根据海水淡化工艺需要增减数量，中段闪蒸器中第二海水槽能够根据海水淡化工艺需要加装烟气余热回收装置用以利用海水加热器高温侧排出的烟气。
所述末级闪蒸器由第三外壳、风扇、布水器、格栅、第三海水槽、第三海水泵六部分组成，所述风扇用于增加扰动提高格栅表面海水蒸发速度；
所述淡水储罐采用密封舱体，其上部装有排气阀门定期抽真空为海水淡化工艺淡水侧提供负压；
所述中段闪蒸器能够根据工艺要求的蒸发量相应增减其数量，第十五三通阀门、第十六三通阀门、第十七三通阀门用于旁通末级闪蒸器。
所述控制系统包括第一三通阀门、第二三通阀门、第三三通阀门、第四三通阀门、第五三通阀门、第六三通阀门、第七三通阀门、第八三通阀门、第九三通阀门、第十三通阀门、第十一三通阀门、第十二三通阀门、第十三三通阀门、第十四三通阀门、第十五三通阀门、第十六三通阀门、第十七三通阀门、第一旁通阀门、第二旁通阀门、第一中间工质泵、第二中间工质泵、第一海水泵、第二海水泵、第三海水泵、第四海水泵、压缩机配套的变频执行机构和控制器及配套电力电子设施。
基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站的运行方法，当电网要求动力电站进行满负荷运行，系统选择工作模式一：
此时电网要求系统满负荷出力或者电价处在高位，系统主动进入最高输出模式，海水淡化工艺进入最低耗电模式；根据以上所述，通过控制系统调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉通过CO 2加热器为一级超临界CO 2布雷顿循环提供热量， 通过CO 2预热器为二级超临界CO 2布雷顿循环提供热量，一级二级超临界CO 2布雷顿循环联合运行共用二级回热器并通过第一三通阀门、第二三通阀门实现两个布雷顿循环的流量分配；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器和海水预热器传递给海水；另一部分是锅炉排放的烟气通过海水加热器进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器、中段闪蒸器；在此工作模式下可通过锅炉、储热罐以及CO 2循环流量在合理范围内调整热动力系统出力；
当电网要求动力电站减少出力，为工作模式二：
此时电网要求系统降低出力或者电价处在较高位，系统主动进入较高输出模式，海水淡化工艺进入中档耗电模式。根据以上所述，通过控制系统调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉CO 2加热器为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器和海水预热器传递给海水；另一部分是锅炉排放的烟气通过海水加热器进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器、中段闪蒸器、末级闪蒸器，末级闪蒸器中的风扇处在常闭状态；在此工作模式下可通过锅炉、储热罐以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量；
当电网要求动力电站继续减少出力，为工作模式三：
此时电网要求系统继续降低出力或者电价处在中位，系统主动进入较低输出模式，海水淡化工艺进入中档耗电模式，根据以上所述，通过控制系统调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉通过CO 2加热器为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通，在工作模式二基础上系统进一步将二级回热器旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器和海水预热器传递给海水；另一部分是锅炉排放的烟气通过海水加热器进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器、中段闪蒸器、末级闪蒸器，末级闪蒸器中的风扇处在常闭状态；在此工作模式下可通过锅炉、储热罐以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量；
当电网要求动力电站以最低负荷运行，为工作模式四：
此时电网要求系统低负荷出力或者电价处在低位，系统主动进入最低输出模式，海水淡化工艺进入最高耗电模式；根据以上所述，通过控制系统调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉通过CO 2预热器为二级超临界CO 2布雷顿循环提供热量，原系统重构成二级超临界CO 2布雷顿循环叠加CO 2冷却循环，一级超临界CO 2布雷顿循环被旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器和海水预热器传递给海水；另一部分是锅炉排放的烟气通过海水加热器进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器、中段闪蒸器、末级闪蒸器，末级闪蒸器中的风扇处在常开状态；在此工作模式下可通过锅炉、储热罐以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时进一步增加了高淡水产量。
本发明有如下有益效果：
1、本发明所述超临界CO 2布雷顿循环不同于传统的回热型循环、再热型循环、再压缩循环和中间冷却等，传统超临界CO 2布雷顿循环的改进型是在低压状态下分流在高压状态下汇流，本发明所述超临界CO 2布雷顿循环低压状态下分流在低压状态下汇流，并在传统 运行高低压之外生成了一个第三级压力并可以在一定范围内进行调节，可以更充分的利用CO 2压缩设备和膨胀设备的可调性大大提高系统输出灵活性。
2、本发明所述海水淡化系统在传统多级闪蒸系统之上加以改进，首先在初级闪蒸器、中段闪蒸器中填充鹅卵石增加水蒸气发生速度，末级闪蒸器中结合空调冷却塔技术，通过结合布水器、格栅和风扇增加能量消耗以提升低温段水蒸气发生速度。
3、本发明在充分开发CO 2压缩和膨胀设备尺寸小、可调能力强的优势，辅以可调海水淡化系统，不仅可实现火力发电系统的大范围可调，还为调节过程中产生的过于热量以及系统本身不能利用的热量提供一连续可变的热负载，进一步提升热动力发电的经济效益，除海水淡化以外还可应用于其他苦咸水淡化场景。
4、本发明的工况模式一适应场景为当电网要求动力电站进行满负荷运行或电价最高时，一级、二级超临界CO 2布雷顿循环联合运行，海水淡化系统以最小耗电量运行，用以配合电网波动要求或实现最大经济效益。
5、本发明的工况模式二该模式适应场景为当电网要求动力电站进一步降低出力或者电价处在较高位系统主动进入较高输出模式，一级超临界CO 2布雷顿循环独立运行海水淡化工艺进入中档耗电量运行，用以配合电网波动要求或实现最大经济效益。
6、本发明在工况模式三适应场景为当电网要求动力电站继续降低出力或者电价处在中位系统主动进入较低输出模式，一级超临界CO 2布雷顿循环独立运行且去掉二级回热工艺海水淡化工艺进入中档耗电量运行，用以配合电网波动要求或实现最大经济效益。
7、本发明在工况模式四，该模式适应场景为当电网要求动力电站低负荷出力或者电价处在低位系统主动进入最低输出模式，二级超临界CO 2布雷顿循环叠加CO 2冷却循环运行海水淡化工艺进入最高耗电模式，用以配合电网波动要求或实现最大经济效益。
附图说明
下面结合附图和实施例对本发明作进一步说明。
图1本发明超临界二氧化碳动力循环结合海水淡化的高灵活性电、水联合生产系统。
图2本发明实施例的电、水联合生产系统工作模式一示意图。
图3本发明实施例的电、水联合生产系统工作模式二示意图。
图4本发明实施例的电、水联合生产系统工作模式三示意图。
图5本发明实施例的电、水联合生产系统工作模式四示意图。
图6本发明热源结合储热系统第一状态示意图。
图7本发明热源结合储热系统第二状态示意图。
图8本发明初级闪蒸器结构示意图。
图9本发明中段闪蒸器结构示意图。
图10本发明末级闪蒸器结构视图。
图11本发明末级闪蒸器结构透视图。
图12本发明淡水储罐示意图。
图中：一级膨胀机1a、二级膨胀机1b、一级压缩机2a、二级压缩机2b、CO2加热器3a、CO2预热器3b、一级回热器4a、二级回热器4b、CO2冷却器5、海水加热器6a、海水预热器6b、蒸 汽冷凝器6c、锅炉7、储热罐8、控制器9、第一三通阀门10a、第二三通阀门10b、第三三通阀门10c、第四三通阀门10d、第五三通阀门10e、第六三通阀门10g、第七三通阀门10h、第八三通阀门10i、第九三通阀门10j、第十三通阀门10k、第十一三通阀门10l、第十二三通阀门10m、第十三三通阀门10n、第十四三通阀门10p、第十五三通阀门10q、第十六三通阀门10r、第十七三通阀门10s、第一旁通阀10f、第二旁通阀10o、第一中间工质泵11a、第二中间工质泵11b、淡水泵11c、第一海水泵11d、第二海水泵11e、第三海水泵11f、第四海水泵11g、初级闪蒸器12、中段闪蒸器13、末级闪蒸器14、淡水储罐15、第一外壳21、第二外壳31、第三外壳41、密封舱体51、第一低温冷凝器22、第二低温冷凝器32、第一冷凝水盘23、第二冷凝水盘33、第一海水槽24、第二海水槽34、第三海水槽45、第一低温海水进口25a、第二低温海水进口35a、第一低温海水出口25b、第二低温海水出口35b、第一水蒸气出口25c、第二水蒸气出口35c、第一淡水出口25d、第二淡水出口35d、第一高温海水进口25e、第二高温海水进口35e、第一高温海水出口25f、第二高温海水出口35f、风扇42、布水器43、格栅44、排气阀门52。
具体实施方式
下面结合附图对本发明的实施方式做进一步的说明。
实施例1：
请参阅图1-12，一种基于超临界二氧化碳动力循环结合海水淡化的高灵活性电、水联合生产系统，由锅炉7、储热罐8、CO 2加热器3a、CO 2预热器3b、海水加热器6a和第一工质泵11a、第二中间工质泵11b设备组成的热源循环系统；由CO 2加热器3a、CO 2预热器3b、一级膨胀机1a、二级膨胀机1b、一级压缩机2a、二级压缩机2b、一级回热器4a、二级回热器4b和CO 2冷却器5设备组成的热动力循环系统；由CO 2冷却器5、海水加热器6a、海水预热器6b、蒸汽冷凝器6c、初级闪蒸器12、中段闪蒸器13、末级闪蒸器14、淡水储罐15、淡水泵11c、第一海水泵11d、第二海水泵11e、第三海水泵11f、第四海水泵11g等设备组成的海水淡化系统；第一三通阀门10a、第二三通阀门10b、第三三通阀门10c、第四三通阀门10d、第五三通阀门10e、第六三通阀门10g、第七三通阀门10h、第八三通阀门10i、第九三通阀门10j、第十三通阀门10k、第十一三通阀门10l、第十二三通阀门10m、第十三三通阀门10n、第十四三通阀门10p、第十五三通阀门10q、第十六三通阀门10r、第十七三通阀门10s，第一旁通阀10f、第二旁通阀10o，各泵、压缩机配套的变频执行机构和控制器9构成的控制系统；
如图1，锅炉7通过CO 2加热器3a和CO 2预热器3b为动力循环提供热量，并在加热循环管路并联一储热罐8，并通过控制第二中间工质泵11b、第二旁通阀10o、第十二三通阀门和第十三三通阀门来实现在体统调节过程中配合进行储热和提热；所述动力循环通过CO 2加热器3a和CO 2预热器3b从热源吸热，并通过超临界CO 2布雷顿循环实现热电转换，并通过第一三通阀门10a、第二三通阀门10b、第三三通阀门10c、第四三通阀门10d、第五三通阀门10e、第六三通阀门10g、第七三通阀门10h、第八三通阀门10i、第九三通阀门10j、第十三通阀门10k、第十一三通阀门10l调节实现四种主要工作模式：工作模式一(一级、二级超临界CO 2布雷顿循环联合运行)，工作模式二(一级超临界CO 2布雷顿循环单独运行，带有两级回热)，工作模式三(一级超临界CO 2布雷顿循环单独运行，带有一级回热)和工作模式四(二级超临界CO 2布雷顿循环单独运行)，其中一级、二级超临界CO 2布雷顿循环联共用二级回热器4b并通过第一三通阀门10a、第二三通阀门10b进行二者流量的分配；当动力循环工作模式发生变 化或在固定模式内进行输出调节时动力循环吸热量和废热放热量会发生变化，而锅炉7和储热罐8又无法迅速响应就要求海水淡化系统亦随之进行调节；海水淡化工艺主要热源来源于海水预热器6b所传递的动力循环放出的废热和海水加热器6a所传递的锅炉烟气余热，低温海水通过回收闪蒸装置中的冷凝热进一步提高能源利用效率，水蒸气发生装置使海水淡化工艺的核心主要有：初级闪蒸器12、中段闪蒸器13、末级闪蒸器14其中中段闪蒸器13可根据负荷需要进行数量的增减，末级末级闪蒸器14包含风扇42可主动增加蒸发速度，因此相配套的海水淡化也有三级工作模式：低耗电工作模式(初级闪蒸器12、中段闪蒸器13联合运行)，中档耗电工作模式(初级闪蒸器12、中段闪蒸器13、末级闪蒸器14、风扇42不开启)，高耗电工作模式(初级闪蒸器12、中段闪蒸器13、末级闪蒸器14、风扇42开启)。
实施例2：
如图2，当电网要求动力电站进行满负荷运行，系统选择工作模式一：
此时电网要求系统满负荷出力或者电价处在高位系统主动进入最高输出模式，海水淡化工艺进入最低耗电模式；根据以上所述，通过控制器9调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉7热源出口接至CO 2加热器3a高温侧入口、CO 2加热器3a高温侧出口接至CO 2预热器3b高温侧入口、CO 2预热器3b高温侧出口接至锅炉锅炉7热源入口完成对整个动力循环提供热量；此时CO 2加热器3a为一级超临界CO 2布雷顿循环提供热量，CO 2预热器3b为二级超临界CO 2布雷顿循环提供热量；其中，一级超临界CO 2布雷顿循环的循环介质CO 2经CO 2加热器3a低温侧进口并在其内部被加热后，由CO 2加热器3a低温侧出口进入一级膨胀机1a进口并在其内部膨胀并输出功后，由一级膨胀机1a出口进入一级回热器4a高温侧进口并在其内放出富余热量后，由一级回热器4a高温侧出口进入第一三通阀门10a进口并在其内与来自二级超临界CO 2布雷顿循环的CO 2进行汇流后，由第一三通阀门10a出口进入二级回热器4b高温侧进口并其内放出富余热量后，由二级回热器4b高温侧出口进入第二三通阀门10b进口并在其内分流一股进行二级超临界CO 2布雷顿循环另一股继续进行一级超临界CO 2布雷顿循环进入CO 2冷却器5高温侧进口并其内放出富余热量后，由CO 2冷却器5高温侧出口进入一级压缩机2a进口并在其内受到外界做过增压后，由一级压缩机2a出口进入二级回热器4b低温侧进口并其内回收高温侧热量后，由二级回热器4b低温侧出口进入一级回热器4a低温侧进口并其内回收高温侧热量后，由一级回热器4a低温侧出口进入CO 2加热器3a低温侧进口完成一级超临界CO 2布雷顿循环；二级超临界CO 2布雷顿循环的循环介质CO 2在第二三通阀门10b内分流除进入一级超临界CO 2布雷顿循环外的流体其余部分进入二级压缩机2b进口并在其内受到外界做过增压后，由二级压缩机2b出口进入CO 2预热器3b低温侧进口并在其内被加热后，由CO 2预热器3b低温侧出口进入二级膨胀机1b进口在其内部膨胀并输出功后，由二级膨胀机1b出口进入第一三通阀门10a进口在其内与来自一级超临界CO 2布雷顿循环的CO 2进行汇流后，由第一三通阀门10a出口进入二级回热器4b高温侧进口并其内放出富余热量后，由二级回热器4b高温侧出口进入第二三通阀门10b进口并在其内分流一股进行一级超临界CO 2布雷顿循环另一股继续进行二级超临界CO 2布雷顿循环进入二级压缩机2b进口完成二级超临界CO 2布雷顿循环；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，软化水通过淡水泵11c升压从水泵11c出口进入CO 2冷却器5低温侧入口并在其内部吸收动力循环排放的冷却热量后，由CO 2冷却器5低温侧出口进入海水预热器6b高温侧入口并在其内部将热量传递给海水后，由海水预热器6b高温侧出口进入淡水泵11c入 口完成循环；锅炉7排放烟气由海水加热器6a高温侧进口并在其内部放热加热海水后由海水加热器6a高温侧出口排放；原始低温海水通过蒸汽冷凝器6c低温侧进口并在其内部回收水蒸气的冷凝热后，由蒸汽冷凝器6c低温侧出口进入中段闪蒸器13中的低温冷凝器33进口35a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器33出口35b进入初级闪蒸器12中的低温冷凝器23进口25a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器23出口25b进入第一海水泵11d进口在其内提升压力后，由第一海水泵11d出口进入(多余海水经第十四三通阀门10p分流后排放)海水预热器6b低温侧进口并在其内部吸收动力循环排放的冷却热量后，由海水预热器6b低温侧出口进入海水加热器6a低温侧进口并在其内部吸收锅炉7的烟气余热后，由海水加热器6a低温侧出口进入初级闪蒸器12海水槽24入口25e并在其内部闪蒸后，浓缩海水由初级闪蒸器12海水槽24底部出口25f进入第二海水泵11e入口并在其内部升压后，由第二海水泵11e出口进入中段闪蒸器13海水槽34入口35e并在其内部闪蒸后，浓缩海水由中段闪蒸器13海水槽34底部出口35f进入第四海水泵11g排放，其中初级闪蒸器12中闪蒸蒸汽接触初级闪蒸器12中的低温冷凝器23凝结出的淡水通过初级闪蒸器12中的冷凝水盘23收集后由冷凝水盘23出口25d进入淡水储罐15，初级闪蒸器12中闪蒸蒸汽未冷凝部分由初级闪蒸器12蒸汽出口25c进入中段闪蒸器13蒸汽入口并在其内与中段闪蒸器13中的闪蒸蒸汽混合后，蒸汽接触中段闪蒸器13中的低温冷凝器33凝结出的淡水通过中段闪蒸器13中的冷凝水盘33收集后由冷凝水盘33出口35d进入淡水储罐15，中段蒸器13中蒸汽未冷凝部分由中级闪蒸器13蒸汽出口35c进入蒸汽冷凝器6c高温侧入口并在其内部放热冷凝后，冷凝淡水由蒸汽冷凝器6c高温侧出口进入淡水储罐15；在此工作模式下可通过锅炉7、储热罐8以及CO 2循环流量在合理范围内调整热动力系统出力。
实施例3：
如图3，当电网要求动力电站减少出力，系统选择工作模式二：
此时电网要求系统降低出力或者电价处在较高位系统主动进入较高输出模式，海水淡化工艺进入中档耗电模式。根据以上所述，通过控制器9调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉7热源出口接至CO 2加热器3a高温侧入口、CO 2加热器3a高温侧出口接至锅炉7热源入口(通过调节阀门组第十一三通阀门和第十二三通阀门联动CO 2预热器3b高温侧被直接旁通掉)完成对整个动力循环提供热量；此时CO 2加热器3a为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通；其中，一级超临界CO 2布雷顿循环的循环介质CO 2经CO 2加热器3a低温侧进口并在其内部被加热后，由CO 2加热器3a低温侧出口进入一级膨胀机1a进口并在其内部膨胀并输出功后，由一级膨胀机1a出口进入一级回热器4a高温侧进口并在其内放出富余热量后，由一级回热器4a高温侧出口进入二级回热器4b高温侧进口并其内放出富余热量后，由二级回热器4b高温侧出口进入CO 2冷却器5高温侧进口并其内放出富余热量后，由CO 2冷却器5高温侧出口进入一级压缩机2a进口并在其内受到外界做过增压后，由一级压缩机2a出口进入二级回热器4b低温侧进口并其内回收高温侧热量后，由二级回热器4b低温侧出口进入一级回热器4a低温侧进口并其内回收高温侧热量后，由一级回热器4a低温侧出口进入CO 2加热器3a低温侧进口完成一级超临界CO 2布雷顿循环；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，软化水通过淡水泵11c升压从水泵11c出口进入CO 2冷却器5低温侧入口并在其内部吸收动力循环排放的冷却 热量后，由CO 2冷却器5低温侧出口进入海水预热器6b高温侧入口并在其内部将热量传递给海水后，由海水预热器6b高温侧出口进入淡水泵11c入口完成循环；锅炉7排放烟气由海水加热器6a高温侧进口并在其内部放热加热海水后由海水加热器6a高温侧出口排放；原始低温海水通过蒸汽冷凝器6c低温侧进口并在其内部回收水蒸气的冷凝热后，由蒸汽冷凝器6c低温侧出口进入中段闪蒸器13中的低温冷凝器33进口35a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器33出口35b进入初级闪蒸器12中的低温冷凝器23进口25a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器23出口25b进入第一海水泵11d进口在其内提升压力后，由第一海水泵11d出口进入(多余海水经第十四三通阀门10p分流后排放)海水预热器6b低温侧进口并在其内部吸收动力循环排放的冷却热量后，由海水预热器6b低温侧出口进入海水加热器6a低温侧进口并在其内部吸收锅炉7的烟气余热后，由海水加热器6a低温侧出口进入初级闪蒸器12海水槽24入口25e并在其内部闪蒸后，浓缩海水由初级闪蒸器12海水槽24底部出口25f进入第二海水泵11e入口并在其内部升压后，由第二海水泵11e出口进入中段闪蒸器13海水槽34入口35e并在其内部闪蒸后，浓缩海水由中段闪蒸器13海水槽34底部出口35f进入第三海水泵11f入口并在其内部升压后，由第三海水泵11f出口进入末级闪蒸器14布水器43入口46a并经由布水器43格栅44进一步浓缩的海水汇至末级闪蒸器14海水槽45从其底部进入第四海水泵11g排放，其中初级闪蒸器12中闪蒸蒸汽接触初级闪蒸器12中的低温冷凝器23凝结出的淡水通过初级闪蒸器12中的冷凝水盘23收集后由冷凝水盘23出口25d进入淡水储罐15，初级闪蒸器12中蒸汽未冷凝部分由初级闪蒸器12蒸汽出口25c进入中段闪蒸器13蒸汽入口并在其内与中段闪蒸器13中的闪蒸蒸汽混合后，蒸汽接触中段闪蒸器13中的低温冷凝器33凝结出的淡水通过中段闪蒸器13中的冷凝水盘33收集后由冷凝水盘33出口35d进入淡水储罐15，中段闪蒸器13中蒸汽未冷凝部分经由第十五三通阀10q进口与末级闪蒸器14中的闪蒸蒸汽混合后，由第十五三通阀10q出口进入蒸汽冷凝器6c高温侧入口并在其内部放热冷凝后，冷凝淡水由蒸汽冷凝器6c高温侧出口进入淡水储罐15。在此工作模式下可通过锅炉7、储热罐8以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量。
实施例4：
如图4，当电网要求动力电站继续减少出力，系统选择工作模式三：
此时电网要求系统进一步降低出力或者电价处在中位系统主动进入中档输出模式，海水淡化工艺进入中档耗电模式。根据以上所述，通过控制器9调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉7热源出口接至CO 2加热器3a高温侧入口、CO 2加热器3a高温侧出口接至锅炉7热源入口(通过调节阀门组第十一三通阀门和第十二三通阀门联动CO 2预热器3b高温侧被直接旁通掉)完成对整个动力循环提供热量；此时CO 2加热器3a为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通；其中，一级超临界CO 2布雷顿循环的循环介质CO 2经CO 2加热器3a低温侧进口并在其内部被加热后，由CO 2加热器3a低温侧出口进入一级膨胀机1a进口并在其内部膨胀并输出功后，由一级膨胀机1a出口进入一级回热器4a高温侧进口并在其内放出富余热量后，由一级回热器4a高温侧出口进入CO 2冷却器5高温侧进口并其内放出富余热量(通过阀门组第一三通阀10a、第一旁通阀10f和第二三通阀10b联动直接旁通掉二级回热器4b高温侧)后，由CO 2冷却器5高温侧出口进入一级压缩机2a进口并在其内受到外界做过增压后，由一级压缩机2a出口进入一级回热器4a低温 侧进口(通过阀门组第三三通阀10c和第四三通阀10d联动直接旁通掉二级回热器4b低温侧)并在其内部回收高温侧热量后，由一级回热器4a低温侧出口进入CO 2加热器3a低温侧进口完成一级超临界CO 2布雷顿循环；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，软化水通过淡水泵11c升压从水泵11c出口进入CO 2冷却器5低温侧入口并在其内部吸收动力循环排放的冷却热量后，由CO 2冷却器5低温侧出口进入海水预热器6b高温侧入口并在其内部将热量传递给海水后，由海水预热器6b高温侧出口进入淡水泵11c入口完成循环；锅炉7排放烟气由海水加热器6a高温侧进口并在其内部放热加热海水后由海水加热器6a高温侧出口排放；原始低温海水通过蒸汽冷凝器6c低温侧进口并在其内部回收水蒸气的冷凝热后，由蒸汽冷凝器6c低温侧出口进入中段闪蒸器13中的低温冷凝器33进口35a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器33出口35b进入初级闪蒸器12中的低温冷凝器23进口25a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器23出口25b进入第一海水泵11d进口在其内提升压力后，由第一海水泵11d出口进入(多余海水经第十四三通阀门10p分流后排放)海水预热器6b低温侧进口并在其内部吸收动力循环排放的冷却热量后，由海水预热器6b低温侧出口进入海水加热器6a低温侧进口并在其内部吸收锅炉7的烟气余热后，由海水加热器6a低温侧出口进入初级闪蒸器12，的第一海水槽24入口25e并在其内部闪蒸后，浓缩海水由初级闪蒸器12的第一海水槽24底部出口25f进入第二海水泵11e入口并在其内部升压后，由第二海水泵11e出口进入中段闪蒸器13的第二海水槽34入口35e并在其内部闪蒸后，浓缩海水由中段闪蒸器13的是第二海水槽34底部出口35f进入第三海水泵11f入口并在其内部升压后，由第三海水泵11f出口进入末级闪蒸器14布水器43入口46a并经由布水器43格栅44进一步浓缩的海水汇至末级闪蒸器14的第三海水槽45从其底部进入第四海水泵11g排放，其中初级闪蒸器12中闪蒸蒸汽接触初级闪蒸器12中的低温冷凝器23凝结出的淡水通过初级闪蒸器12中的冷凝水盘23收集后由冷凝水盘23出口25d进入淡水储罐15，初级闪蒸器12中蒸汽未冷凝部分由初级闪蒸器12蒸汽出口25c进入中段闪蒸器13蒸汽入口并在其内与中段闪蒸器13中的闪蒸蒸汽混合后，蒸汽接触中段闪蒸器13中的低温冷凝器33凝结出的淡水通过中段闪蒸器13中的冷凝水盘33收集后由冷凝水盘33出口35d进入淡水储罐15，中段闪蒸器13中蒸汽未冷凝部分经由第十五三通阀10q进口与末级闪蒸器14中的闪蒸蒸汽混合后，由第十五三通阀10q出口进入蒸汽冷凝器6c高温侧入口并在其内部放热冷凝后，冷凝淡水由蒸汽冷凝器6c高温侧出口进入淡水储罐15。在此工作模式下可通过锅炉7、储热罐8以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量。
实施例5：
如图5，当电网要求动力电站进行最低负荷运行，系统选择工作模式四：
此时电网要求系统低负荷出力或者电价处在低位系统主动进入最低输出模式，海水淡化工艺进入最高耗电模式；根据以上所述，通过控制器9调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉7热源出口接至CO 2预热器3b高温侧入口(通过调节阀门组第八三通阀10i和第九三通阀10j联动CO 2加热器3a高温侧直接被旁通)、CO 2预热器3b高温侧出口接至锅炉7热源入口完成对整个动力循环提供热量；此时CO 2预热器3b为二级超临界CO 2布雷顿循环提供热量，一级超临界CO 2布雷顿循环被旁通；其中，二级超临界CO 2布雷顿循环的循环介质CO 2经CO 2预热器3b低温侧进口并在其内部被加热后，由CO 2预热器3b低温侧出口 进入二级膨胀机1b进口并在其内部膨胀并输出功后，由二级膨胀机1b出口进入二级回热器4b高温侧进口并在其内放出富余热量后，由二级回热器4b高温侧出口进入二级压缩机2b进口并在其内受到外界做过增压完成二级超临界CO 2布雷顿循环，并建立一个CO 2冷却循环其中CO 2流体进入二级回热器4b低温侧进口并在其内吸收高温侧热量后，由二级回热器4b低温侧出口进入进入CO 2冷却器5高温侧进口并其内放出富余热量后，由CO 2冷却器5高温侧出口进入一级压缩机2a进口并在其内受到外界做过增压后，由一级压缩机2a出口进入二级回热器4b低温侧进口完成CO 2冷却循环(通过调节阀门组第一三通阀10a、第二三通阀10b、第三三通阀10c、第四三通阀10d和第五三通阀10e联动使CO 2加热器3a、一级回热器4a和一级膨胀机1a旁通并将系统重构成二级超临界CO 2布雷顿循环叠加CO 2冷却循环)；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，软化水通过淡水泵11c升压从水泵11c出口进入CO 2冷却器5低温侧入口并在其内部吸收动力循环排放的冷却热量后，由CO 2冷却器5低温侧出口进入海水预热器6b高温侧入口并在其内部将热量传递给海水后，由海水预热器6b高温侧出口进入淡水泵11c入口完成循环；锅炉7排放烟气由海水加热器6a高温侧进口并在其内部放热加热海水后由海水加热器6a高温侧出口排放；原始低温海水通过蒸汽冷凝器6c低温侧进口并在其内部回收水蒸气的冷凝热后，由蒸汽冷凝器6c低温侧出口进入中段闪蒸器13中的低温冷凝器33进口35a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器33出口35b进入初级闪蒸器12中的低温冷凝器23进口25a并在其内部回收水蒸气的冷凝热后，由中段闪蒸器13中的低温冷凝器23出口25b进入第一海水泵11d进口在其内提升压力后，由第一海水泵11d出口进入(多余海水经第十四三通阀门10p分流后排放)海水预热器6b低温侧进口并在其内部吸收动力循环排放的冷却热量后，由海水预热器6b低温侧出口进入海水加热器6a低温侧进口并在其内部吸收锅炉7的烟气余热后，由海水加热器6a低温侧出口进入初级闪蒸器12的第一海水槽24入口25e并在其内部闪蒸后，浓缩海水由初级闪蒸器12的第一海水槽24底部出口25f进入第二海水泵11e入口并在其内部升压后，由第二海水泵11e出口进入中段闪蒸器13的第三海水槽34入口35e并在其内部闪蒸后，浓缩海水由中段闪蒸器13的第三海水槽34底部出口35f进入第三海水泵11f入口并在其内部升压后，由第三海水泵11f出口进入末级闪蒸器14布水器43入口46a并经由布水器43格栅44进一步浓缩的海水汇至末级闪蒸器14的第三海水槽45从其底部进入第四海水泵11g排放，其中初级闪蒸器12中闪蒸蒸汽接触初级闪蒸器12中的低温冷凝器23凝结出的淡水通过初级闪蒸器12中的冷凝水盘23收集后由冷凝水盘23出口25d进入淡水储罐15，初级闪蒸器12中蒸汽未冷凝部分由初级闪蒸器12蒸汽出口25c进入中段闪蒸器13蒸汽入口并在其内与中段闪蒸器13中的闪蒸蒸汽混合后，蒸汽接触中段闪蒸器13中的低温冷凝器33凝结出的淡水通过中段闪蒸器13中的冷凝水盘33收集后由冷凝水盘33出口35d进入淡水储罐15，中段闪蒸器13中蒸汽未冷凝部分经由第十五三通阀10q进口与末级闪蒸器14中的闪蒸蒸汽混合后，由第十五三通阀10q出口进入蒸汽冷凝器6c高温侧入口并在其内部放热冷凝后，冷凝淡水由蒸汽冷凝器6c高温侧出口进入淡水储罐15。在此工作模式下可通过锅炉7、储热罐8以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量此时末级闪蒸器14中的风扇42常开。
如图6-7，储热罐8有三种运行工况储热工况提热工况和关闭工况，在储热工况下中间工质在锅炉7内加热后由锅炉7入口进入第六三通阀门10g分流后主要部分用于加热热 动力循环，过余部分进入中间工质泵11b进口并在其内部升压后，由中间工质泵11b出口进入储热罐8进口并在其内部放热后，由储热罐出口进入第七三通阀门10h与完成加热热动力循环的流体混合后回到锅炉7；在提热工况下中间工质在完成加热热动力循环后在第七三通阀门10h出分流一部分流入锅炉7进口并在其内吸热后，由锅炉7出口进入第六三通阀门10g，另一部分流入储热罐8进口并在其内吸热后，由储热罐8出口进入第六三通阀门10g(通过调节阀门组第十二三通阀门10m、第十三三通阀门10n和第二旁通阀门10o联动旁通中间工质泵11b)，两股流体在第六三通阀门10g汇流后去加热热动力循环；在关闭工况下通过调节阀门组第六三通阀门10g和第七三通阀门10h联动旁通中间工质泵11b和储热罐8；基于超临界二氧化碳动力循环结合海水淡化的高灵活性电、水联合生产系统在工作模式一、工作模式二、工作模式三和工作模式四下稳定运行时储热罐8处在关闭工况，系统在高电力输出模式向低电力输出模式切换(如工作模式一向工作模式二切换)或在特定工作模式下系统调节流量降低电力输出而锅炉又不能快速降低热量输出时储热罐8处在储热工况，系统在低电力输出模式向高电力输出模式切换或在特定工作模式下系统调节流量提升电力输出而锅炉又不能快速提升热量输出时储热罐8处在储热工况。
如图8-9，所述初级闪蒸器12由第一外壳21、第一低温冷凝器22、第一冷凝水盘23、第一海水槽24、第二海水泵11e五个部分组成，所述初级闪蒸器12包含第一低温海水进口25a、第一低温海水出口25b、第一水蒸气出口25c、第一淡水出口25d、第一高温海水进口25e和第一高温海水出口25f六个接口，其中所述第一海水槽24中堆砌鹅卵石提高出气速度，所述第一冷凝水盘23底部引出第一淡水出口25d用以排出冷凝水；
进一步的，所述初级闪蒸器12中闪蒸出的水蒸气，接触初级闪蒸器12中的第一低温冷凝器22冷凝成淡水并由初级闪蒸器12中的第一冷凝水盘23收集最终汇聚至淡水储罐15，剩余蒸汽流入中段闪蒸器13并与中段闪蒸器13中闪蒸出的水蒸气混合，接触与中段闪蒸器13中的低温冷凝器32冷凝成淡水并由与中段闪蒸器13中的第二冷凝水盘33收集最终汇聚至淡水储罐15，剩余蒸汽通过第十五三通阀门10q与末级闪蒸器14中扩容闪蒸出的水蒸气混合进入蒸汽冷凝器6c高温侧放热冷凝最终汇入淡水储罐15；
进一步的，所述中段闪蒸器13由第二外壳31、第二低温冷凝器32、第二冷凝水盘33、第二海水槽34、第三海水泵11f五个部分组成，所述中段闪蒸器13包含第二低温海水进口35a、第二低温海水出口35b、第二水蒸气出口35c、第二淡水出口35d、第二高温海水进口35e和第二高温海水出口35f六个接口，其中所述第二海水槽34中堆砌鹅卵石提高出气速度，所述第二冷凝水盘33底部引出第二淡水出口35d用以排出冷凝水，与初级闪蒸器12不同的是中段闪蒸器13能够根据海水淡化工艺需要增减数量，中段闪蒸器13中第二海水槽34能够根据海水淡化工艺需要加装烟气余热回收装置用以利用海水加热器6a高温侧排出的烟气。
如图10-11，所述末级闪蒸器14由第三外壳41、风扇42、布水器43、格栅44、第三海水槽45、第三海水泵11f六部分组成，所述风扇42用于增加扰动提高格栅44表面海水蒸发速度。
如图12，所述淡水储罐15采用密封舱体51，其上部装有排气阀门52定期抽真空为海水淡化工艺淡水侧提供负压；
所述中段闪蒸器13能够根据工艺要求的蒸发量相应增减其数量，第十五三通阀门10q、第十六三通阀门10r、第十七三通阀门10s用于旁通末级闪蒸器14。

Claims (10)

  1. 一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：它包括热源循环系统、热动力循环系统、海水淡化系统和控制系统；
    所述热源循环系统与热动力循环系统和海水淡化系统系统相连，并分别为其提供工作过程中所需要的热源；
    所述控制系统同时与热源循环系统、热动力循环系统和海水淡化系统的各个执行机构相连，并控制其相应工作。
  2. 根据权利要求1所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述热源循环系统包括锅炉(7)、储热罐(8)、CO 2加热器(3a)、CO 2预热器(3b)、海水加热器(6a)、第二旁通阀门(10o)、第六三通阀门(10g)、第七三通阀门(10h)、第八三通阀门(10i)、第九三通阀门(10j)、第十三通阀门(10k)、第十一三通阀门(10l)、第十二三通阀门(10m)、第十三三通阀门(10n)、第一中间工质泵(11a)、第二中间工质泵(11b)和配套管理；
    所述锅炉(7)为系统原始热源，锅炉(7)与CO 2加热器(3a)和CO 2预热器(3b)串联，并为热动力循环系统提供热量；锅炉(7)与海水加热器(6a)相连，并为海水淡化系统提供热量；
    所述储热罐(8)并联在CO 2加热器(3a)、CO 2预热器(3b)构成的串联换热器组两侧，用以调节锅炉换热过程中由于热惰性与负载CO 2加热器(3a)、CO 2预热器(3b)存在的不匹配问题；
    所述第一中间工质泵(11a)和第二中间工质泵(11b)分别与热动力循环系统和储热罐(8)相连，并分别用于调节加热热动力循环系统和储热罐(8)的流量分配；所述第十二三通阀门(10m)、第十三三通阀门(10n)和第二旁通阀门(10o)和第二中间工质泵(11b)并连，并实现储热罐(8)的吸放热以及流量调节；
    所述第八三通阀门(10i)、第九三通阀门(10j)用以旁通CO 2加热器(3a)的高温侧、第十三通阀门(10k)、第十一三通阀门(10l)用以旁通CO 2预热器(3b)的高温侧来实现热动力循环的大范围灵活性调控。
  3. 根据权利要求2所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述储热罐(8)储热材料选用熔融盐或液态金属，根据电力系统要求当系统负荷下降，锅炉热量不能快速调节时，将部分热量储存在储热罐(8)，当系统负荷上升，锅炉热量不能快速调节时，则提出储热罐(8)中储存的热量为动力循环补充热量；
    所述CO 2加热器(3a)、CO 2预热器(3b)和海水加热器(6a)采用直接内置安装在锅炉(7)内，去掉中间介质直接加热CO 2或海水。
  4. 根据权利要求1所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述热动力循环系统包括CO 2加热器(3a)、CO 2预热器(3b)、一级膨胀机(1a)、二级膨胀机(1b)、一级压缩机(2a)、二级压缩机(2b)、一级回热器(4a)、二级回热器(4b)、CO 2冷却器(5)、第一旁通阀门(10f)、第一三通阀门(10a)、第二三通阀门(10b)、第三三通阀门(10c)、第四三通阀门(10d)、第五三通阀门(10e)和配套管路；
    所述热动力循环系统采用CO 2为工质，其嵌套了两级超临界CO 2布雷顿循环：包括一级超临界CO 2布雷顿循环和二级超临界CO 2布雷顿循环；CO 2加热器(3a)为所述一级超临界CO 2布雷顿循环提供热量，之后通过CO 2预热器(3b)为所述二级超临界CO 2布雷顿循环提供热量，量实现了一级、二级超临界CO 2布雷顿循环间接结合与能量的梯级利用。
  5. 根据权利要求4所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力 电站，其特征在于：所述一级超临界CO 2布雷顿循环的循环工质为超临界CO 2，CO 2工质先后流经一级压缩机(2a)、二级回热器(4b)低温侧、一级回热器(4a)低温侧、CO 2加热器(3a)低温侧、一级膨胀机(1a)、一级回热器(4a)高温侧、第一三通阀门(10a)、二级回热器(4b)高温侧、第二三通阀门(10b)、CO 2冷却器(5)高温侧、一级压缩机(2a)完成循环，相对应的CO 2流体先后经历了升压、吸热、吸热、吸热、膨胀、放热、汇流、放热、分流、放热、升压几个工艺实现吸热并做工的整体工艺流程；
    所述二级超临界CO 2布雷顿循环的循环工质为超临界CO 2，CO 2工质先后流经二级压缩机(2b)、CO 2预热器(3b)低温侧、二级膨胀机(1b)、第一三通阀门(10a)、二级回热器(4b)高温侧、第二三通阀门(10b)、二级压缩机(2b)完成循环，相对应的CO 2流体先后经历了升压、吸热、膨胀、汇流、放热、分流、升压几个工艺实现吸热并做工的整体工艺流程；
    所述一级、二级超临界CO 2布雷顿循环通过第一三通阀门(10a)、第二三通阀门(10b)和二级回热器(4b)实现上述一级、二级超临界CO 2布雷顿循环的直接相互结合，通过第一三通阀门(10a)、第二三通阀门(10b)调节二级循环的分流比例来调整系统运行；
    所述第一三通阀门(10a)、第二三通阀门(10b)和第一旁通阀门(10f)用于旁通二级超临界CO 2布雷顿循环使一级超临界CO 2布雷顿循环独立运行，所述第三三通阀门(10c)、第四三通阀门(10d)、第五三通阀门(10e)用于旁通一级超临界CO 2布雷顿循环使二级超临界CO 2布雷顿循环独立运行；
    一级膨胀机(1a)、二级膨胀机(1b)、一级压缩机(2a)、二级压缩机(2b)之间为满足调节工况采用变速器加离合器的链接方式；CO 2加热器(3a)、CO 2预热器(3b)、一级回热器(4a)、二级回热器(4b)、CO2冷却器(5)使用印刷电路板换热器。
  6. 根据权利要求1所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述海水淡化系统包括CO 2冷却器(5)、海水加热器(6a)、海水预热器(6b)、蒸汽冷凝器(6c)、初级闪蒸器(12)、中段闪蒸器(13)、末级闪蒸器(14)、淡水储罐(15)、第十四三通阀门(10p)、第十五三通阀门(10q)、第十六三通阀门(10r)、第十七三通阀门(10s)、淡水泵(11c)、第一海水泵(11d)、第二海水泵(11e)、第三海水泵(11f)、第四海水泵(11g)和配套管路；
    所述海水加热器(6a)、海水预热器(6b)、蒸汽冷凝器(6c)采用抗腐蚀堵、塞能力较强、对压力要求不高、经济性好的管壳式换热器，换热器内换热管束采用铜管；
    加热海水的热量来源于三部分，包括通过蒸汽冷凝器(6c)、中段闪蒸器(13)、初级闪蒸器(12)回收海水闪蒸后携带的冷凝热，通过海水预热器(6b)回收热动力循环末端冷却的热量，通过海水加热器(6a)回收热源循环中烟气废热，其中利用软化水先后流经淡水泵(11c)、CO 2冷却器(5)低温侧、海水预热器(6b)高温侧、淡水泵(11c)，对应完成升压、吸热、放热、升压的循环工艺，将热动力循环末端冷却放出的热量间接传递给海水，其中软化水循环主要是为了保护CO 2冷却器(5)所采用的印刷电路板换热器，或者采用简化系统，简化后直接用一台换热器将动力循环末端的冷却热量直接用于加热海水；
    抽取自然的低温海水先后流经蒸汽冷凝器(6c)低温侧、中段闪蒸器(13)中的低温冷凝器(32)、初级闪蒸器(12)中的低温冷凝器(22)、第一海水泵(11d)、至第十四三通阀门(10p)、海水预热器(6b)低温侧、海水加热器(6a)低温侧、初级闪蒸器(12)的第一海水槽(24)、第二海水泵11e、中段闪蒸器(13)的第二海水槽(34)、第三海水泵(11f)、末级闪蒸器 (14)中布水器(43)格栅(44)和第三海水槽(45)、第四海水泵(11g)排放完成海水浓缩，相对应的海水流体先后经历了吸热、吸热、吸热、升压、分流、吸热、吸热、闪蒸浓缩、升压、闪蒸浓缩、升压、扩容闪蒸浓缩、升压排放几个工艺实现吸热低压闪蒸浓缩的工艺流程。
  7. 根据权利要求6所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述初级闪蒸器(12)由第一外壳(21)、第一低温冷凝器(22)、第一冷凝水盘(23)、第一海水槽(24)、第二海水泵(11e)五个部分组成，所述初级闪蒸器(12)包含第一低温海水进口(25a)、第一低温海水出口(25b)、第一水蒸气出口(25c)、第一淡水出口(25d)、第一高温海水进口(25e)和第一高温海水出口(25f)六个接口，其中所述第一海水槽(24)中堆砌鹅卵石提高出气速度，所述第一冷凝水盘(23)底部引出第一淡水出口(25d)用以排出冷凝水；
    所述初级闪蒸器(12)中闪蒸出的水蒸气，接触初级闪蒸器(12)中的第一低温冷凝器(22)冷凝成淡水并由初级闪蒸器(12)中的第一冷凝水盘(23)收集最终汇聚至淡水储罐(15)，剩余蒸汽流入中段闪蒸器(13)并与中段闪蒸器(13)中闪蒸出的水蒸气混合，接触与中段闪蒸器(13)中的低温冷凝器(32)冷凝成淡水并由与中段闪蒸器(13)中的第二冷凝水盘(33)收集最终汇聚至淡水储罐(15)，剩余蒸汽通过第十五三通阀门(10q)与末级闪蒸器(14)中扩容闪蒸出的水蒸气混合进入蒸汽冷凝器(6c)高温侧放热冷凝最终汇入淡水储罐(15)；
    所述中段闪蒸器(13)由第二外壳(31)、第二低温冷凝器(32)、第二冷凝水盘(33)、第二海水槽(34)、第三海水泵(11f)五个部分组成，所述中段闪蒸器(13)包含第二低温海水进口(35a)、第二低温海水出口(35b)、第二水蒸气出口(35c)、第二淡水出口(35d)、第二高温海水进口(35e)和第二高温海水出口(35f)六个接口，其中所述第二海水槽(34)中堆砌鹅卵石提高出气速度，所述第二冷凝水盘(33)底部引出第二淡水出口(35d)用以排出冷凝水，与初级闪蒸器(12)不同的是中段闪蒸器(13)能够根据海水淡化工艺需要增减数量，中段闪蒸器(13)中第二海水槽(34)能够根据海水淡化工艺需要加装烟气余热回收装置用以利用海水加热器(6a)高温侧排出的烟气。
  8. 根据权利要求6所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述末级闪蒸器(14)由第三外壳(41)、风扇(42)、布水器(43)、格栅(44)、第三海水槽(45)、第三海水泵(11f)六部分组成，所述风扇(42)用于增加扰动提高格栅(44)表面海水蒸发速度；
    所述淡水储罐(15)采用密封舱体(51)，其上部装有排气阀门(52)定期抽真空为海水淡化工艺淡水侧提供负压；
    所述中段闪蒸器(13)能够根据工艺要求的蒸发量相应增减其数量，第十五三通阀门(10q)、第十六三通阀门(10r)、第十七三通阀门(10s)用于旁通末级闪蒸器(14)。
  9. 根据权利要求1所述一种基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站，其特征在于：所述控制系统包括第一三通阀门(10a)、第二三通阀门(10b)、第三三通阀门(10c)、第四三通阀门(10d)、第五三通阀门(10e)、第六三通阀门(10g)、第七三通阀门(10h)、第八三通阀门(10i)、第九三通阀门(10j)、第十三通阀门(10k)、第十一三通阀门(10l)、第十二三通阀门(10m)、第十三三通阀门(10n)、第十四三通阀门(10p)、第十五三通阀门(10q)、第十六三通阀门(10r)、第十七三通阀门(10s)、第一旁通阀门(10f)、第二旁通 阀门(10o)、第一中间工质泵(11a)、第二中间工质泵(11b)、第一海水泵(11d)、第二海水泵(11e)、第三海水泵(11f)、第四海水泵(11g)、压缩机配套的变频执行机构和控制器(9)及配套电力电子设施。
  10. 采用权利要求1-9任意一项所述基于超临界二氧化碳动力循环结合海水淡化的灵活性动力电站的运行方法，其特征在于，当电网要求动力电站进行满负荷运行，系统选择工作模式一：
    此时电网要求系统满负荷出力或者电价处在高位，系统主动进入最高输出模式，海水淡化工艺进入最低耗电模式；根据以上所述，通过控制系统(9)调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉(7)通过CO 2加热器(3a)为一级超临界CO 2布雷顿循环提供热量，通过CO 2预热器(3b)为二级超临界CO 2布雷顿循环提供热量，一级二级超临界CO 2布雷顿循环联合运行共用二级回热器(4b)并通过第一三通阀门(10a)、第二三通阀门(10b)实现两个布雷顿循环的流量分配；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器(5)和海水预热器(6b)传递给海水；另一部分是锅炉(7)排放的烟气通过海水加热器(6a)进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器(12)、中段闪蒸器(13)；在此工作模式下可通过锅炉(7)、储热罐(8)以及CO 2循环流量在合理范围内调整热动力系统出力；
    当电网要求动力电站减少出力，为工作模式二：
    此时电网要求系统降低出力或者电价处在较高位，系统主动进入较高输出模式，海水淡化工艺进入中档耗电模式；
    根据以上所述，通过控制系统(9)调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉(7)CO 2加热器(3a)为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器(5)和海水预热器(6b)传递给海水；另一部分是锅炉(7)排放的烟气通过海水加热器(6a)进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器(12)、中段闪蒸器(13)、末级闪蒸器(14)，末级闪蒸器(14)中的风扇(42)处在常闭状态；在此工作模式下可通过锅炉(7)、储热罐(8)以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量；
    当电网要求动力电站继续减少出力，为工作模式三：
    此时电网要求系统继续降低出力或者电价处在中位，系统主动进入较低输出模式，海水淡化工艺进入中档耗电模式，根据以上所述，通过控制系统(9)调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉(7)通过CO 2加热器(3a)为一级超临界CO 2布雷顿循环提供热量，二级超临界CO 2布雷顿循环被旁通，在工作模式二基础上系统进一步将二级回热器(4b)旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器(5)和海水预热器(6b)传递给海水；另一部分是锅炉(7)排放的烟气通过海水加热器(6a)进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器(12)、中段闪蒸器(13)、末级闪蒸器(14)，末级闪蒸器(14)中的风扇(42)处在常闭状态；在此工作模式下可通过锅炉(7)、储热罐(8)以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时适当增加海水流量以提高淡水产量；
    当电网要求动力电站以最低负荷运行，为工作模式四：
    此时电网要求系统低负荷出力或者电价处在低位，系统主动进入最低输出模式，海水淡化工艺进入最高耗电模式；根据以上所述，通过控制系统(9)调节各阀门泵等执行机构和既有管路实现如下工艺环节，锅炉(7)通过CO 2预热器(3b)为二级超临界CO 2布雷顿循环提供热量，原系统重构成二级超临界CO 2布雷顿循环叠加CO 2冷却循环，一级超临界CO 2布雷顿循环被旁通；海水淡化工艺所用热源来自于热动力循环无法利用的低品位热源，一部分由CO 2冷却器(5)和海水预热器(6b)传递给海水；另一部分是锅炉(7)排放的烟气通过海水加热器(6a)进一步提高海水温度，此时水蒸气的发生装置为初级闪蒸器(12)、中段闪蒸器(13)、末级闪蒸器(14)，末级闪蒸器(14)中的风扇(42)处在常开状态；在此工作模式下可通过锅炉(7)、储热罐(8)以及CO 2循环流量在合理范围内调整热动力系统出力，于此同时进一步增加了高淡水产量。
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