WO2017185930A1 - 高效太阳能海水淡化与空调制冷联合运行方法与系统 - Google Patents

高效太阳能海水淡化与空调制冷联合运行方法与系统 Download PDF

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WO2017185930A1
WO2017185930A1 PCT/CN2017/078024 CN2017078024W WO2017185930A1 WO 2017185930 A1 WO2017185930 A1 WO 2017185930A1 CN 2017078024 W CN2017078024 W CN 2017078024W WO 2017185930 A1 WO2017185930 A1 WO 2017185930A1
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steam
seawater
air conditioning
heat
heat exchange
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PCT/CN2017/078024
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English (en)
French (fr)
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殷占民
张岩丰
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武汉凯迪工程技术研究总院有限公司
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Publication of WO2017185930A1 publication Critical patent/WO2017185930A1/zh

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    • 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
    • C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B27/00—Machines, plants or systems, using particular sources of energy
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/007—Modular design
    • 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
    • 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
    • Y02A20/138—Water desalination using renewable energy
    • Y02A20/142—Solar thermal; Photovoltaics
    • 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
    • Y02A20/20—Controlling water pollution; Waste water treatment
    • Y02A20/208—Off-grid powered water treatment
    • Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems

Definitions

  • the invention relates to a new energy technology, in particular to a high-efficiency solar seawater desalination and air conditioning refrigeration combined operation method and system.
  • Desalination of seawater also known as desalination and desalination of seawater, refers to the process of removing excess salt and minerals from water to obtain fresh water, and is an open source incremental technology for realizing water use.
  • the development and industrial application of desalination technology has a history of half a century. During this period, industrial technologies represented by multi-stage flashing, multi-effect evaporation and reverse osmosis have been formed.
  • Multi-effect evaporation is the evaporation of heated seawater in a plurality of evaporators connected in series.
  • the vapor evaporated from the previous evaporator acts as a heat source for the next evaporator and condenses into fresh water.
  • the multi-stage flash seawater desalination is to evaporate the heated seawater in sequence in a plurality of flash chambers whose pressure is gradually lowered, and condense the steam to obtain fresh water.
  • the reverse osmosis method uses a semi-permeable membrane that only allows the solvent to pass through and does not allow the solute to permeate, and separates the seawater from the fresh water.
  • seawater desalination requires a large amount of energy, and the use of conventional power sources and heat sources for seawater desalination has high operating costs and poor economic returns.
  • Absorption refrigeration is the use of certain pairs of working fluids with special properties.
  • the absorption and release of one substance to another produces a state change of the substance, which is accompanied by an endothermic and exothermic process.
  • the absorption refrigerating machine uses the solution to precipitate the vapor of the low-boiling component under certain conditions, and under another condition, it can strongly absorb the low-boiling component vapor to complete the refrigeration cycle.
  • a binary solution is often used as the working medium. It is customary to say that the low-boiling component is a refrigerant, and the high-boiling component is an absorbent, and the two form a working pair.
  • the currently widely used working fluids are only ammonia-water and lithium bromide-aqueous solutions, the former for cryogenic systems and the latter for air-conditioning systems.
  • the lithium bromide absorption type air conditioner uses lithium bromide solution as an absorbent and water as a refrigerant, and uses water to evaporate and absorb heat under high vacuum to achieve the purpose of refrigeration.
  • the evaporated refrigerant water vapor is absorbed by the lithium bromide solution, and the solution is thinned. This process occurs in the absorber, and then the solution is heated by the heat energy.
  • the water is separated and the solution is thickened, which is carried out in the generator.
  • Generator charge There is a lithium bromide solution and the pressure is low. When heated slightly, the water evaporates from the lithium bromide solution.
  • the evaporated water vapor is condensed in the condenser to become refrigerant water.
  • the refrigerant water evaporates in the evaporator, taking away the heat inside it.
  • the evaporated water vapor is absorbed by the lithium bromide solution in the absorber, and the lithium bromide solution which absorbs the water vapor is diluted and heated and evaporated in the generator, so that the circulation is continuously performed to realize the air conditioning refrigeration.
  • the lithium bromide absorption type air conditioner Due to the direct utilization of thermal energy, the lithium bromide absorption type air conditioner has a large heat exhausting load, and a large amount of cooling water is required for heat exchange cooling in the condensation and absorption process.
  • the Chinese patent "a solar air-conditioning seawater desalination system” discloses a solar air-conditioning seawater desalination system, which comprises: a solar heat collecting device, a seawater desalination device and a refrigerating device, and a lithium bromide concentrator lithium bromide solution absorbing heat
  • the generated steam enters the evaporating absorber through a heat exchanger after being condensed into fresh water through a lithium bromide evaporator tube, and the lithium bromide solution in the lithium bromide concentrator enters the evaporating absorber through a heat exchanger; the lithium bromide in the evaporating absorber
  • the solution enters the first-effect evaporator as a heat source for seawater desalination, and the concentrated lithium bromide solution enters the lithium bromide concentrator.
  • the invention utilizes steam generated by evaporation of a lithium bromide solution as a heat source for seawater desalination, thereby improving energy utilization of solar energy.
  • the disadvantage is that the heat absorption in the shell side of the lithium bromide evaporator generates negative pressure steam into the first-effect seawater desalination evaporator, the low-pressure steam temperature is low, and the desalination of the seawater needs to adopt the low-temperature multi-effect flashing method, and the practical application transformation requirements High; desalination depends on the steam provided by the air conditioning system.
  • the air conditioning system is deactivated, seawater desalination cannot be performed. If the air conditioning system is idling, the service life of the air conditioning system is reduced.
  • the object of the present invention is to provide a high-efficiency solar seawater desalination and air-conditioning refrigeration combined operation method and system with high energy utilization rate and low transformation requirements, and use solar energy as a heat source to realize air-conditioning refrigeration while seawater desalination.
  • the present invention provides a high-efficiency solar seawater desalination and air conditioning refrigeration combined operation method, including a solar heat collecting step, a seawater desalination step, and an air conditioning refrigeration step.
  • the solar heat collecting step the solar energy is subjected to photothermal conversion, and the generated heat is transferred to the heat transfer working medium.
  • the seawater desalination step the seawater is heated and distilled by using the heat transfer medium obtained by the solar heat collecting step as a heat source, and the obtained distilled steam is further condensed with seawater to obtain fresh water.
  • the distillation steam obtained by the seawater desalination step is delivered to The absorption air conditioning system heats the refrigerant pair as a heat source steam.
  • the distilled steam transfers heat to the refrigerant working medium pair, and then returns to the seawater desalination step, further condenses with seawater to obtain fresh water, and preheats the seawater.
  • the absorption air conditioning system absorbs the heat released during the cooling process through the cooling medium circulation, and the cooling working medium whose temperature rises after the heat is absorbed exchanges heat with the seawater in the seawater desalination step, and transfers the heat to the sea water.
  • the cooling medium is cooled and the seawater is preheated.
  • the distillation is carried out in series using a multi-stage distiller, and the seawater is sequentially passed through a primary distiller, a secondary distiller, and subsequent distillers.
  • the seawater is heated by the heat transfer medium obtained by the solar heat collecting step in the primary distiller and the second distiller, and the steam generated by the primary distiller is passed into the absorption air conditioning system as the heat source steam,
  • the steam generated by the distillers after the stage (including the second stage) and before the final stage (excluding the final stage) is passed to the next-stage distiller to heat the seawater, and the partially condensed steam after heating and the final distiller evaporate.
  • the generated steam is then condensed with seawater to obtain fresh water.
  • the invention also provides a high-efficiency solar seawater desalination and air conditioning refrigeration combined operation system designed to implement the foregoing method, comprising a solar heat collection system, a seawater desalination system and an absorption air conditioning system.
  • the solar heat collecting system includes a solar heat collector, and the solar heat collector may be various collectors such as a flat plate type collector and a vacuum tube collector.
  • the solar collector is provided with a heat transfer working fluid input port of the heat collecting system and a heat transfer working medium output port of the heat collecting system.
  • the seawater desalination system comprises a distillation system and a heat exchange system, and the distillation system can adopt a conventional single-stage or two-stage distillation method, and can also adopt a multi-stage distillation and a multi-effect distillation method.
  • the heat exchange system uses partition wall heat exchange, such as tubular heat exchangers and plate heat exchangers.
  • the distillation system comprises at least one distiller, the distillation system is provided with a distillation system seawater input port, a distillation system brine outlet, a distillation system steam outlet, a distillation system heat transfer medium input port, and a distillation system heat transfer medium output. mouth.
  • the heat exchange system comprises a steam condensing device and an air conditioning cooling device; the heat exchange system is provided with a seawater input port of the heat exchange system and a seawater output port of the heat exchange system; the steam condensing device is provided with a distillation steam input port of the heat exchange system, The air conditioner returns to the steam input port and the fresh water outlet of the heat exchange system; the air conditioner cooling device is provided with a heat exchange system air conditioner cooling working fluid input port and a heat exchange system air conditioner cooling working fluid output port.
  • the heat exchange system distillation steam input port and the air conditioner return steam input port are disposed at a high temperature side inlet of the steam condensing device, and the heat exchange system fresh water outlet is disposed at a high temperature side outlet of the steam condensing device, and the heat exchange system air conditioner is cooled
  • the working fluid input port and the heat exchange system air conditioner cooling working fluid output port are disposed at both ends of the high temperature side of the air conditioner cooling device. Both ends of the low temperature side of the steam condensing device and the low temperature side ends of the air conditioning cooling device are respectively provided with a seawater input port and a seawater output port.
  • the absorption air conditioning system can adopt a single-effect or multi-effect absorption air conditioning system, usually a whole machine installation, and an air conditioner for introducing heated steam is disposed thereon.
  • the system heats the steam input port, the air conditioning system heating steam output port for discharging the partially condensed steam after heating, and the air conditioning system cooling medium input port for the air conditioner cooling and the air conditioning system cooling working fluid output port, the cooling worker
  • the cooling water is usually used, and other cooling medium can be used if necessary.
  • the heat transfer working fluid inlet of the heat collecting system is connected to the heat transfer working fluid outlet of the distillation system, and the heat transfer working fluid outlet of the heat collecting system is connected to the heat transfer working fluid inlet of the distillation system.
  • the seawater inlet of the distillation system is connected to the seawater outlet of the heat exchange system.
  • the air conditioning system heating steam input port and the heat exchange system distillation steam input port are respectively connected to the distillation system steam output port, and the air conditioning system heating steam output port is connected to the air conditioner return steam input port.
  • the heat exchange system air conditioner cooling working fluid input port is connected to the air conditioning system cooling working fluid output port, and the heat exchange system air conditioner cooling working fluid output port is connected to the air conditioning system cooling working fluid input port.
  • the system is also equipped with a number of pumps, gauges and valves as required, using conventional designs.
  • the heat exchange system is further provided with a brine heat exchange device for preheating seawater by using brine obtained by distillation, wherein the high temperature side of the brine heat exchange device is provided with a heat exchange system brine input port and a heat exchange system brine output.
  • the bottom side of the brine heat exchange device is provided with a seawater input port and a seawater outlet, and the brine input port of the heat exchange system is connected to the brine output port of the distillation system.
  • the distillation system employs a single stage distillation comprising only a primary distiller, a distillation system seawater input port, a distillation system brine outlet, a distillation system steam outlet, a distillation system heat transfer medium input port, distillation
  • the system heat transfer medium output ports are all set on the primary distiller.
  • the distillation system adopts two-stage distillation, and is composed of a first-stage distiller and a two-stage distiller.
  • the distillation system seawater input port and the distillation system heat transfer medium input port are disposed on the primary distiller.
  • the distillation system brine outlet and the distillation system heat transfer working outlet are arranged on the secondary distiller.
  • the distillation system steam outlet includes an air outlet steam outlet disposed on the primary distiller and an evaporative vapor outlet disposed on the secondary distiller.
  • the seawater outlet of the primary distiller is connected to the seawater inlet of the secondary distiller, and the heat transfer working outlet of the primary distiller is connected to the heat transfer working inlet of the secondary distiller.
  • the steam outlet for the air conditioner is connected to the heating steam input port of the air conditioning system, and the vapor steam outlet is connected to the distillation steam input port of the heat exchange system.
  • the distillation system employs a multi-stage distillation comprising at least three distillers, the first two distillers being a primary distiller and a second distiller according to the direction of seawater flow, and the last distiller is a final distillation Device.
  • the distillation system seawater input port and the distillation system heat transfer medium input port are disposed on the primary distiller, and the distillation system heat transfer working fluid outlet is disposed on the secondary distiller, and the primary distiller is passed The hot working fluid outlet is connected to the heat transfer working inlet of the secondary distiller.
  • the distillation system brine outlet is disposed on the final distiller.
  • Seawater of various distillers The outlet is connected to the seawater inlet of the next-stage distiller, and the steam outlet of each distiller after the second stage (including the second stage) and before the final stage (excluding the final stage) and the heating steam of the distiller of the next stage
  • the input ports are connected, and the steam generated in the stage is used to heat the seawater in the lower distiller.
  • the pressure in the distillers of each stage is gradually reduced, so that the temperature of the upper stage steam is higher than the boiling point of the seawater in the next stage distiller, and the lower stage distiller can be heated.
  • the distillation system steam outlet comprises a steam outlet for air conditioning disposed on the primary distiller, a heated steam outlet disposed on each of the distillers after (excluding) the secondary distiller, and is disposed at the final stage Evaporative vapor outlet on the distiller.
  • the steam outlet for the air conditioner is connected to the heating steam input port of the air conditioning system.
  • the heating steam outlet and the evaporation steam outlet are connected to the distillation steam input port of the heat exchange system.
  • the steam condensing device comprises a fresh water condenser and a steam heat exchanger
  • the air conditioning cooling device comprising a seawater cooling heat exchanger
  • the brine heat exchange device comprises a brine cooling heat exchanger.
  • the low temperature sides of the fresh water condenser, the seawater cooling heat exchanger, the brine cooling heat exchanger, and the steam heat exchanger are connected in series in series.
  • the seawater input port of the heat exchange system is disposed at a low temperature side input end of the fresh water condenser, and the sea water output port of the heat exchange system is disposed at a low temperature side output end of the steam heat exchanger.
  • the heat exchange system distillation steam input port is disposed at a high temperature side input end of the fresh water condenser, and the air conditioner return steam input port is disposed at a high temperature side input end of the steam heat exchanger.
  • the brine input port of the heat exchange system and the brine outlet of the heat exchange system are respectively disposed at two ends of the high temperature side of the brine cooling heat exchanger.
  • the fresh water outlet of the heat exchange system is disposed at a high temperature side output end of the fresh water condenser and the steam heat exchanger.
  • the heat exchange system air conditioner cooling working fluid input port and the heat exchange system air conditioner cooling working fluid output port are disposed at both ends of the high temperature side of the seawater cooling heat exchanger.
  • the system further comprises a fresh water tank for collecting condensed water, the fresh water tank being provided with a fresh water collecting port and an uncondensed steam outlet, the fresh water collecting port being connected to the fresh water outlet of the heat exchange system.
  • the uncondensed steam outlet is connected to a steam condensing device of the heat exchange system.
  • the absorption air conditioning system is a single-effect or multi-effect lithium bromide air conditioner.
  • the absorption air conditioning system is a double effect lithium bromide air conditioner
  • the absorption air conditioning system includes a high voltage generator, a low voltage generator, a condenser, an evaporator, and an absorber.
  • the air conditioning system heating steam input port and the air conditioning system heating steam output port are disposed on the high voltage generator, and the solution output end of the high voltage generator is connected to the solution input end of the low pressure generator.
  • a primary steam output of the high pressure generator is coupled to a primary steam input of the low pressure generator, the secondary steam output of the low pressure generator being coupled to a secondary steam input of the condenser, the low pressure generator
  • the primary steam condensate output is connected to the primary steam condensate input of the condenser
  • the refrigerant output of the condenser is connected to the refrigerant input of the evaporator
  • the vapor output of the evaporator is Absorber
  • the steam input is connected.
  • the solution output end of the absorber is connected to the solution input end of the high pressure generator, and a low temperature heat exchanger and a high temperature heat exchanger are disposed therebetween, and the solution output end of the absorber and the low temperature side of the low temperature heat exchanger
  • the low temperature side of the high temperature heat exchanger and the solution input end of the high pressure generator are connected in sequence.
  • the solution output end of the high pressure generator, the high temperature side of the high temperature heat exchanger, and the solution input end of the low pressure generator are sequentially connected, the solution output end of the low pressure generator, the high temperature side of the low temperature heat exchanger, and the solution of the absorber The inputs are connected in sequence.
  • the cooling medium input port of the air conditioning system, the cooling heat exchange device of the condenser, the cooling heat exchange device of the absorber, and the cooling medium output port of the air conditioning system are sequentially connected.
  • a cold water heat exchanger is disposed in the evaporator, and two ends of the cold water heat exchanger are respectively provided with an air conditioning system cold water input port and an air conditioning system cold water output port, and a lower portion of the evaporator is provided with a circulating refrigerant output end.
  • An upper portion is provided with a circulating refrigerant input end, and a refrigerant pump is disposed between the circulating refrigerant output end and the circulating refrigerant input end.
  • a heat transfer medium circulation pump is disposed between the solar collector and the heat transfer working fluid inlet of the distillation system.
  • the solar collector is a medium-high temperature collector.
  • seawater desalination uses solar energy to generate steam, and the generated steam is used as a heat source of the absorption air conditioning system, which can fully realize the cascade utilization of energy, and has high utilization efficiency; 2) the cooling medium of the absorption air conditioning system The heat exchange cooling by seawater and the preheating of seawater not only save the cooling water of the absorption air conditioning system, but also fully recover the waste heat of the absorption air conditioning system, thereby achieving a substantial increase in the thermal efficiency of the entire system; 3) the solar energy is clean Energy, environmentally friendly, zero-emission, solar-driven seawater desalination and air conditioning joint operation, can fully utilize solar energy, is conducive to environmental protection, and has great social, environmental and economic benefits.
  • FIG. 1 is a schematic diagram of a process flow of a high-efficiency solar seawater desalination and air conditioning refrigeration combined operation system designed by the present invention.
  • FIG. 2 is a schematic structural view of the solar heat collecting system of FIG.
  • Figure 3 is a schematic view showing the structure of the absorption type air conditioning system of Figure 1 when single-effect heating is used.
  • Figure 4 is a schematic view showing the structure of the absorption type air conditioning system of Figure 1 when multi-effect heating is used.
  • Figure 5 is a schematic view showing the structure of the distillation system of Figure 1 when it is heated by the first stage.
  • Figure 6 is a schematic view showing the structure of the distillation system of Figure 1 when it is heated by two stages.
  • Figure 7 is a schematic view showing the structure of the distillation system of Figure 1 when it is heated by three stages.
  • Figure 8 is a schematic structural view of the heat exchange system of Figure 1.
  • Figure 9 is another schematic structural view of the heat exchange system of Figure 1.
  • Embodiment 10 is a schematic view showing the overall structure of Embodiment 1.
  • high pressure generator 1 air conditioning system heating steam input port 1.1, air conditioning system heating steam output port 1.2, low pressure generator 2, condenser 3, air conditioning system cooling fluid output port 3.1, evaporator 4, refrigerant pump 5, Cold water pump 6, terminal air conditioning equipment 7, absorber 8, air conditioning system cooling medium input port 8.1, solvent pump 9, low temperature heat exchanger 10, high temperature heat exchanger 11, steam heat exchanger 12, brine pump 13, final stage Distillator 14, secondary distiller 15, primary distiller 16, solar collector 17, heat transfer medium input port 17.1, heat transfer system heat transfer output 17.2, heat transfer circulating pump 18.
  • the high-efficiency solar seawater desalination and air-conditioning refrigeration combined operation system designed by the invention comprises a solar heat collecting system I, a seawater desalination system II and an absorption air conditioning system III.
  • the main part of the solar heat collecting system I is the solar heat collector 17, which adopts a medium and high temperature collector.
  • the solar heat collector 17 is provided with a heat collecting medium heat input port 17.1, a heat collecting system heat transfer working output port 17.2 and a heat transfer working medium circulating pump 18.
  • the seawater desalination system II includes a distillation system 27 and a heat exchange system 28.
  • the distillation system 27 includes three distillers, which are respectively steamed according to the direction of seawater flow.
  • the distiller 16, the secondary distiller 15, and the final distiller 14 (in this case, a tertiary distiller).
  • the distillation system 27 is provided with a distillation system seawater input port 27.1, a distillation system brine outlet port 27.2, a distillation system steam outlet port 27.3, a distillation system heat transfer medium input port 27.4, and a distillation system heat transfer medium output port 27.5.
  • the distillation system seawater input port 27.1, the distillation system heat transfer medium input port 27.4 is disposed on the primary distiller 16, the distillation system heat transfer medium output port 27.5 is disposed on the secondary distiller 15, and the primary distiller 16 is passed
  • the hot working fluid outlet is connected to the heat transfer working inlet of the secondary distiller 15.
  • the distillation system brine outlet 27.2 is placed on the final distiller 14.
  • the seawater outlet of each of the distillers is connected to the seawater inlet of the lower distiller, and the steam outlet of the secondary distiller 15 is connected to the heated steam inlet of the final distiller 14, and is produced by the secondary distiller 15
  • the steam heats the seawater in the final distiller 14.
  • the distillation system steam outlet 27.3 comprises an air conditioning steam outlet 27.3a disposed on the primary distiller 16, a heated steam outlet 27.3b disposed on the final distiller 14, and an evaporative vapor outlet 27.3c.
  • the air conditioning steam outlet 27.3a is connected to the air conditioning system heating steam inlet 1.1.
  • the heat exchange system 28 includes a steam condensing device 29, an air conditioning cooling device 30, and a brine heat exchange device 31.
  • the heat exchange system 28 is provided with a heat exchange system seawater input port 28.1, a heat exchange system seawater outlet port 28.2.
  • the steam condensing device 29 is provided with a heat exchange system distillation steam input port 29.1, an air conditioner return steam input port 29.2, and a heat exchange system fresh water outlet port 29.3.
  • the air conditioner cooling device 30 is provided with a heat exchange system air conditioner cooling medium input port 30.1 and a heat exchange system air conditioner cooling medium output port 30.2.
  • the high temperature side of the brine heat exchange device 31 is provided with a heat exchange system brine inlet port 31.1 and a heat exchange system brine outlet port 31.2, and a heat exchange system brine inlet port 31.1 is connected to the distillation system brine outlet port 27.2.
  • the steam condensing unit 29 includes a fresh water condenser 19 and a steam heat exchanger 12
  • the air conditioning cooling unit 30 includes a seawater cooling heat exchanger 21
  • the brine heat exchange unit 31 includes a brine cooling heat exchanger 26.
  • the low temperature side of the fresh water condenser 19, the seawater cooling heat exchanger 21, the brine cooling heat exchanger 26, and the steam heat exchanger 12 are sequentially connected in series.
  • a seawater booster pump 24 is disposed between the seawater cooling heat exchanger 21 and the low temperature side of the brine cooling heat exchanger 26.
  • the seawater input port 28.1 of the heat exchange system is disposed at the low temperature side input end of the fresh water condenser 19, and the sea water pump 22 is disposed before the seawater input port 28.1 of the heat exchange system, and the seawater output port 28.2 of the heat exchange system is disposed at the low temperature side of the steam heat exchanger 12. Output.
  • the heat exchange system distillation steam input port 29.1 comprises a distillation vaporization steam input port 29.1a and a distillation condensing steam inlet port 29.1b, wherein the distillation vaporization steam input port 29.1a is disposed at the high temperature side input end of the fresh water condenser 19, and the distillation condensed steam input
  • the port 29.1b is connected to the fresh water tank 25; the air conditioning return steam input port 29.2 is provided at the high temperature side input end of the steam heat exchanger 12.
  • the heat exchange system brine input port 31.1 and the heat exchange system brine output port 31.2 are respectively disposed at both ends of the high temperature side of the brine cooling heat exchanger 26, and a brine pump 13 is disposed near the brine input port 31.1 of the heat exchange system.
  • Heat exchange system fresh water outlet 29.3 is disposed at the high temperature side output of the fresh water condenser 19 and the steam heat exchanger 12.
  • the heat exchange system air conditioner cooling working fluid input port 30.1, the heat exchange system air conditioner cooling working fluid output port 30.2 is disposed at both ends of the high temperature side of the seawater cooling heat exchanger 21, and the cooling pump is arranged near the heat exchange system air conditioner cooling working fluid output port 30.2 20.
  • the fresh water tank 25 is provided with a fresh water collecting port 25.1 and an uncondensed steam output port 25.2, and a fresh water pump 23 is provided at the fresh water outlet of the fresh water tank 25.
  • the high temperature side of the steam heat exchanger 12, the fresh water outlet of the heat exchange system 29.3 and the distillation condensate steam inlet 29.1b are respectively connected to the fresh water collection port 25.1.
  • the uncondensed steam outlet 25.2 is connected to the fresh water condenser 19.
  • the absorption type air conditioning system III is a double-effect lithium bromide air conditioner, and the absorption type air conditioning system III includes a high voltage generator 1, a low pressure generator 2, a condenser 3, an evaporator 4, and an absorption.
  • the high-pressure generator 1 is provided with an air-conditioning system heating steam input port 1.1 and an air-conditioning system heating steam output port 1.2, and the solution output end of the high-voltage generator 1 is connected to the solution input end of the low-pressure generator 2.
  • the primary steam output of the high pressure generator 1 is connected to the primary steam input of the low pressure generator 2
  • the secondary steam output of the low pressure generator 2 is connected to the secondary steam input of the condenser 3
  • the primary steam of the low pressure generator 2 The condensate output end is connected to the primary steam condensate input end of the condenser 3
  • the refrigerant output end of the condenser 3 is connected to the refrigerant input end of the evaporator 4
  • the steam output end of the evaporator 4 and the steam input of the absorber 8 are connected. Connected to the end.
  • the solution output end of the absorber 8 is connected to the solution input end of the high voltage generator 1, and a low temperature heat exchanger 10 and a high temperature heat exchanger 11 are disposed therebetween, a solution output end of the absorber 8 and a low temperature heat exchanger 10
  • the low temperature side, the low temperature side of the high temperature heat exchanger 11, the solution input end of the high pressure generator 1 are sequentially connected, and the lithium bromide solution in the absorber 8 is sent to the high pressure generator 1 through the solvent pump 9.
  • the solution output end of the high voltage generator 1, the high temperature side of the high temperature heat exchanger 11, and the solution input end of the low pressure generator 2 are sequentially connected, the solution output end of the low pressure generator 2, the high temperature side of the low temperature heat exchanger 10, and the absorber 8
  • the solution inputs are connected in sequence.
  • the cooling medium input port 8.1 of the air conditioning system, the cooling heat exchange device of the condenser 3, the cooling heat exchange device of the absorber 8, and the cooling medium output port 3.1 of the air conditioning system are sequentially connected.
  • the evaporator 4 is provided with a cold water heat exchanger, and two ends of the cold water heat exchanger are respectively provided with an air conditioning system cold water input port and an air conditioning system cold water outlet, respectively, and the cold water outlet and the cold water inlet port on the terminal air conditioner 7 respectively. Connected, wherein the low temperature cold water is circulated through the cold water pump 6.
  • the lower portion of the evaporator 4 is provided with a circulating refrigerant output end, the upper portion is provided with a circulating refrigerant input end, and a refrigerant pump 5 is disposed between the circulating refrigerant output end and the circulating refrigerant input end.
  • the connection relationship between the input and output ports of each system is as follows: the heat transfer medium input port 17.1 of the heat collecting system is connected to the heat transfer working medium output port 27.5 of the distillation system.
  • the heat transfer medium output port 17.2 of the heat collecting system is connected to the heat transfer medium input port 27.4 of the distillation system.
  • Distillation system seawater input port 27.1 and heat exchange system seawater transport The exit 28.2 is connected.
  • the air conditioning system heating steam input port 1.1 is connected to the air conditioner steam outlet port 27.3a, and the air conditioning system heating steam outlet port 1.2 is connected to the air conditioner return steam input port 29.2.
  • the distillation evaporation steam input port 29.1a and the distilled condensate steam input port 29.1b are respectively connected to the evaporation steam output port 27.3c and the heating steam output port 27.3b.
  • the heat exchange system air conditioner cooling working fluid input port 30.1 is connected with the air conditioning system cooling working fluid output port 3.1
  • the heat exchange system air conditioner cooling working fluid output port 30.2 is connected with the air conditioning system cooling working fluid input port 8.1.
  • the solar collector 17 absorbs solar energy by photothermal conversion and transfers it to the heat transfer medium (in this case, heat transfer oil), and the heat transfer medium flows into the first distiller 16 and the secondary distiller 15 in turn, and is disposed inside the two distillers.
  • the heat exchanger supplies the required heat to the desalinated seawater, and the heat transfer medium flows out of the secondary distiller 15 and flows back to the solar heat collector 17 through the heat transfer medium circulation pump 18.
  • the seawater flows into the fresh water condenser 19 via the sea water pump 22 to provide a cold source for steam condensation; after the seawater flows out of the fresh water condenser 19, part of the seawater is directly evacuated, and some of the water flows into the seawater cooling heat exchanger 21, the brine heat exchanger 26, and the steam exchange.
  • the heat exchanger 12 separately recovers waste heat from the absorption air conditioner system III, the brine and the air conditioner return steam; the preheated seawater flows into the primary distiller 16 to be distilled, and the distilled concentrated seawater flows into the secondary distiller 15 in sequence, and the final stage The distillation is continued in the distiller 16, and finally, the brine pump 13 flows into the brine heat exchanger 26 to transfer the residual heat to the seawater; the steam distilled from the primary distiller 16 directly serves as the heat source of the absorption air conditioning system III; the secondary distiller 15 distills out The steam enters the final distiller 14 to transfer heat to the concentrated seawater through the heat exchanger therein, and the steam condensed by the final distiller 14 flows into the fresh water tank 25, and the uncondensed steam is partially condensed by the fresh water tank 25
  • the outlet port 25.2 enters the fresh water condenser 19 for further condensation; the steam distilled from the final distiller 14 enters the fresh water condenser 19 to transfer heat to the seawater, and the condensed
  • the steam distilled from the primary distiller 16 is supplied to the high-pressure generator 1 as a heat source of the absorption air-conditioning system III, and heat is transferred to the lithium bromide aqueous solution in the high-pressure generator 1 through the heat exchanger therein, and then passed through the steam heat exchanger. 12 enters the fresh water tank 25 after heat exchange with seawater.
  • the lithium bromide aqueous solution After the lithium bromide aqueous solution is heated and evaporated in the high-pressure generator 1 through the heat exchanger therein, the solution passes through the high-temperature heat exchanger 11 and enters the low-pressure generator 2 to be heated by the heat exchanger therein to further evaporate the water vapor, after the second evaporation
  • the lithium bromide aqueous solution flows out of the low pressure generator 2, and then flows into the absorber 8 through the low temperature heat exchanger 10.
  • the lithium bromide aqueous solution is dissolved and regenerated in the absorber 8 with low-temperature and low-pressure water vapor, and the heat released during the regeneration is removed through the heat exchanger therein.
  • the regenerated lithium bromide aqueous solution in the absorber 8 is pressurized by the solvent pump 9 and sequentially flows into the low
  • the warm heat exchanger 10 and the high temperature heat exchanger 11 perform heat exchange and temperature rise, and finally enter the high voltage generator 1.
  • the water vapor evaporated in the high-pressure generator 1 enters the low-pressure generator 2, and the heat is transferred to the lithium bromide aqueous solution in the low-pressure generator 2 through the heat exchanger in the low-pressure generator 2, and the heat energy therein is recovered, and the heated water vapor is recovered.
  • Condensation into water flows into the condenser 3, and steam generated by heating and evaporation in the low-pressure generator 2 also enters the condenser 3 to be condensed.
  • the refrigerant water collected in the condenser 3 is cooled by the heat exchanger therein and flows into the evaporator 4.
  • the evaporator 4 belongs to a low-temperature vacuum environment, and the refrigerant water therein is pressurized and sprayed back into the evaporator 4 by the refrigerant pump 5, and the water is vaporized in the instantaneous change of the water in the evaporator 4, and is changed in the water vaporization process.
  • the heat is absorbed in the heat exchanger, and the low temperature and low pressure water vapor is absorbed by the lithium bromide aqueous solution in the absorber 8.
  • the heat transfer medium (water in this example) flows into the evaporator 4 through the cold water pump 6, and absorbs the cooling amount through the heat exchanger in the evaporator 4, and then flows into the terminal air conditioner 7, and the terminal air conditioner 7 supplies the user with cooling.
  • the cooling medium flows into the absorber 8 through the cooling pump 20 in sequence, and the condenser 3 passes through the respective internal heat exchangers to be a lithium bromide aqueous solution, and the water is cooled, and then flows into the seawater cooling heat exchanger 21 to transfer the heat to the seawater side and then into the cooling pump. 20, forming a cycle.
  • the distillation system 27 comprises only the primary distiller 16, the distillation system seawater inlet 27.1, the distillation system brine outlet 27.2, the distillation system steam outlet 27.3, the distillation system heat transfer inlet 27.4, the distillation system.
  • the heat transfer medium output ports 27.5 are all disposed on the primary distiller 16. A part of the steam generated by the primary distiller 16 heated by the heat transfer medium is supplied to the absorption type air conditioning system III as a heat source, and the other part is supplied to the steam condensing unit 29 for condensation.
  • the absorption type air conditioning system III is a single-effect lithium bromide air conditioner, which differs from the double-effect lithium bromide air conditioner in that the generator of the air conditioning system has only one (the number 1 of the high voltage generator is used in the figure).
  • the distillation system 27 is composed of a primary distiller 16 and a secondary distiller 15, a distillation system seawater input port 27.1, a distillation system heat transfer medium input port 27.4, which is disposed on the primary distiller 16, a distillation system.
  • the brine outlet 27.2 and the distillation system heat transfer outlet 27.5 are disposed on the secondary distiller 15.
  • the distillation system steam outlet 27.3 comprises an air conditioning steam outlet 27.3a disposed on the primary distiller 16, and an evaporative vapor outlet 27.3c disposed on the secondary distiller 15.
  • the seawater outlet of the primary distiller 16 is connected to the seawater inlet of the secondary distiller 15, and the heat transfer working outlet of the primary distiller 16 is connected to the heat transfer working inlet of the secondary distiller 15.
  • the steam outlet port 27.3a is connected to the air conditioning system heating steam inlet port 1.1
  • the evaporation steam outlet port 27.3c is connected to the heat exchange system distillation steam inlet port 29.1.
  • the heat exchange system (28) is not provided with a steam heat exchanger (12), and the air conditioner return steam input port (29.2) is disposed on the fresh water condenser (19), that is, the return steam directly after the air conditioner is heated The fresh water condenser (19) is cooled.

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Abstract

提供一种高效太阳能海水淡化与空调制冷联合运行方法及系统。该方法包括太阳能集热步骤、海水淡化步骤和空调制冷步骤；海水淡化步骤以太阳能集热步骤中的传热工质作为热源；空调制冷步骤以蒸馏蒸汽作为热源，空调冷却工质通过与海水换热进行冷却。该装置包括太阳能集热系统（I）、海水淡化系统（II）和吸收式空调系统（III）；海水淡化系统（II）包括蒸馏系统（27）和换热系统（28），蒸馏系统（27）通过太阳能集热系统（I）进行加热；吸收式空调系统（III）的加热蒸汽输入口（1.1）与蒸馏系统（I）的蒸汽输出口（27.3）相连通，吸收式空调系统（III）的冷却工质输入口（8.1）、输出口（3.1）分别与换热系统（28）的空调冷却工质输出口（30.2）、输入口（30.1）相连。提供了利用太阳能作为热源实现在海水淡化的同时进行空调制冷，能源利用效率高。

Description

高效太阳能海水淡化与空调制冷联合运行方法与系统 技术领域
本发明涉及一种新能源技术，特别是指一种高效太阳能海水淡化与空调制冷联合运行方法与系统。
背景技术
海水淡化也称海水化淡、海水脱盐，是指将水中的多余盐分和矿物质去除得到淡水的工序，是实现水资源利用的开源增量技术。海水淡化技术的发展与工业应用，已有半个世纪的历史，在此期间形成了以多级闪蒸、多效蒸发和反渗透为主要代表的工业技术。
多效蒸发是让加热后的海水在多个串联的蒸发器中蒸发，前一个蒸发器蒸发出来的蒸汽作为下一蒸发器的热源，并冷凝成为淡水。多级闪蒸海水淡化是将经过加热的海水，依次在多个压力逐渐降低的闪蒸室中进行蒸发，将蒸汽冷凝而得到淡水。反渗透法是利用只允许溶剂透过、不允许溶质透过的半透膜，将海水与淡水分隔开的，如果对海水一侧施加一大于海水渗透压的外压，那么海水中的纯水将反渗透到淡水中。但是，海水淡化需要消耗大量能量，采用传统动力源和热源进行海水淡化的运转成本高，经济效益不佳。
吸收式制冷是利用某些具有特殊性质的工质对，通过一种物质对另一种物质的吸收和释放，产生物质的状态变化，从而伴随吸热和放热过程。吸收式制冷机利用溶液在一定条件下能析出低沸点组分的蒸气，在另一条件下又能强烈地吸收低沸点组分蒸气这一特性完成制冷循环。吸收式制冷机中多采用二元溶液作为工质，习惯上称低沸点组分为制冷剂，高沸点组分为吸收剂，二者组成工质对。人们经过长期的研究，目前获得广泛应用的工质对只有氨——水和溴化锂——水溶液，前者用于低温系统，后者用于空调系统。
溴化锂吸收式空调是以溴化锂溶液为吸收剂，以水为制冷剂，利用水在高真空下蒸发吸热达到制冷的目的。为使制冷过程能连续不断地进行下去，蒸发后的冷剂水蒸气被溴化锂溶液所吸收，溶液变稀，这一过程是在吸收器中发生的，然后以热能为动力，将溶液加热使其水份分离出来，而溶液变浓，这一过程是在发生器中进行的。发生器中充 有溴化锂溶液，且压力较低，稍加热时，水便从溴化锂溶液中蒸发。蒸发出来的水蒸汽在冷凝器中冷凝，成为制冷剂水。制冷剂水在蒸发器中蒸发，带走其内的热量。蒸发出的水气被吸收器中的溴化锂溶液吸收，吸收水气变稀的溴化锂溶液再在发生器中加热蒸发，如此不断循环，实现空调制冷。由于直接利用热能，溴化锂吸收式空调的排热负荷较大，其冷凝和吸收过程中需要使用大量冷却水进行换热冷却。
海水淡化与空调制冷都是耗能大户，需要消耗大量电能或热能。与传统能源相比，太阳能具有安全、环保等优点，将太阳能采集与海水淡化、空调制冷相结合，可大幅降低能源消耗和成本，因而逐渐受到人们重视。
中国专利“一种太阳能空调海水淡化系统”(ZL201310024546.6)公开了一种太阳能空调海水淡化系统，该系统包括：太阳能集热装置、海水淡化装置和制冷装置，溴化锂浓缩器的溴化锂溶液吸热产生的蒸汽进入溴化锂蒸发器管程冷凝成淡水后经换热器进入所述蒸发吸收器，溴化锂浓缩器内的溴化锂溶液经换热器进入所述蒸发吸收器；所述蒸发吸收器内的溴化锂溶液进入溴化锂蒸发器的壳程吸热产生的蒸汽进入首效蒸发器作为海水淡化的热源，浓缩的溴化锂溶液进入溴化锂浓缩器。该发明利用溴化锂溶液蒸发产生的蒸汽作为海水淡化的热源，提高了太阳能的能源利用率。其不足之处在于，溴化锂蒸发器内壳程吸热产生负压蒸汽进入首效海水淡化蒸发器，所述负压蒸汽温度较低，海水淡化需要采用低温多效闪蒸方式，实际应用改造要求高；海水淡化依赖于空调系统提供的蒸汽，空调系统停用时无法进行海水淡化，如果空调系统空转则降低了空调系统使用寿命。
发明内容
本发明的目的在于提供一种能量利用率高、改造要求低的高效太阳能海水淡化与空调制冷联合运行方法与系统，利用太阳能作为热源实现在海水淡化的同时进行空调制冷。
为实现上述目的，本发明所提供的一种高效太阳能海水淡化与空调制冷联合运行方法，包括太阳能集热步骤、海水淡化步骤和空调制冷步骤。所述太阳能集热步骤中，对太阳能进行光热转换，所产生的热量传递给传热工质。所述海水淡化步骤中，以所述太阳能集热步骤获得的传热工质作为热源对海水进行加热蒸馏，所得蒸馏蒸汽再与海水换热后冷凝得到淡水。所述空调制冷步骤中，将所述海水淡化步骤获得的蒸馏蒸汽输送到 吸收式空调系统，作为热源蒸汽对制冷工质对进行加热。该蒸馏蒸汽将热量传递给制冷工质对后，再返回所述海水淡化步骤中，进一步与海水换热冷凝得到淡水，同时对海水进行预热。所述吸收式空调系统通过冷却工质循环吸收在制冷过程中释放的热量，吸收热量后温度升高的冷却工质与所述海水淡化步骤中的海水进行换热，将其中的热量转移到海水中，使所述冷却工质得到冷却，并对海水进行预热。
优选地，所述海水淡化步骤中，采用多级蒸馏器串联的方式进行蒸馏，海水依次通过一级蒸馏器、二级蒸馏器及其后的各级蒸馏器。在一级蒸馏器、二级蒸馏器中通过所述太阳能集热步骤获得的传热工质对海水进行加热，一级蒸馏器产生的蒸汽通入所述吸收式空调系统中作为热源蒸汽，二级以后(含二级)、末级之前(不含末级)的各级蒸馏器产生的蒸汽通入下一级蒸馏器中对海水进行加热，加热后部分冷凝的蒸汽及末级蒸馏器蒸发产生的蒸汽再与海水换热后冷凝得到淡水。
本发明还提供了一种为实现前述方法而设计的高效太阳能海水淡化与空调制冷联合运行系统，包括太阳能集热系统、海水淡化系统和吸收式空调系统。所述太阳能集热系统包括太阳能集热器，该太阳能集热器可采用平板型集热器、真空管集热器等各种集热器。所述太阳能集热器设置有集热系统传热工质输入口和集热系统传热工质输出口。所述海水淡化系统包括蒸馏系统和换热系统，蒸馏系统可采用传统的单级、两级蒸馏方式，也可采用多级蒸馏、多效蒸馏方式。换热系统采用间壁式换热，如管式换热器、板式换热器等。所述蒸馏系统包括至少一个蒸馏器，所述蒸馏系统设置有蒸馏系统海水输入口、蒸馏系统卤水输出口、蒸馏系统蒸汽输出口、蒸馏系统传热工质输入口和蒸馏系统传热工质输出口。所述换热系统包括蒸汽冷凝装置和空调冷却装置；所述换热系统设置有换热系统海水输入口、换热系统海水输出口；所述蒸汽冷凝装置设置有换热系统蒸馏蒸汽输入口、空调返回蒸汽输入口、换热系统淡水输出口；所述空调冷却装置设置有换热系统空调冷却工质输入口和换热系统空调冷却工质输出口。所述换热系统蒸馏蒸汽输入口、空调返回蒸汽输入口设置在蒸汽冷凝装置的高温侧入口，所述换热系统淡水输出口设置在蒸汽冷凝装置的高温侧出口，所述换热系统空调冷却工质输入口和换热系统空调冷却工质输出口设置在空调冷却装置的高温侧两端。所述蒸汽冷凝装置的低温侧两端、空调冷却装置的低温侧两端分别设置有海水输入口和海水输出口。所述吸收式空调系统可采用单效或多效吸收式空调系统，通常为整机安装，其上设置有用于通入加热蒸汽的空调 系统加热蒸汽输入口、用于排出加热后部分冷凝的蒸汽的空调系统加热蒸汽输出口，以及用于空调冷却的空调系统冷却工质输入口和空调系统冷却工质输出口，所述的冷却工质通常采用冷却水，必要时也可采用其他冷却工质。所述集热系统传热工质输入口与蒸馏系统传热工质输出口相连，所述集热系统传热工质输出口与蒸馏系统传热工质输入口相连。所述蒸馏系统海水输入口与换热系统海水输出口相连。所述空调系统加热蒸汽输入口、换热系统蒸馏蒸汽输入口分别与蒸馏系统蒸汽输出口相连，所述空调系统加热蒸汽输出口与空调返回蒸汽输入口相连。所述换热系统空调冷却工质输入口与空调系统冷却工质输出口相连，所述换热系统空调冷却工质输出口与空调系统冷却工质输入口相连。该系统根据需要还设置有若干泵、仪表和阀门等，采用常规设计。
优选地，所述换热系统还设置有利用蒸馏得到的卤水对海水进行预热的卤水换热装置，所述卤水换热装置的高温侧设置有换热系统卤水输入口和换热系统卤水输出口，所述卤水换热装置的低温侧设置有海水输入口和海水输出口，所述换热系统卤水输入口与蒸馏系统卤水输出口相连。
可选地，所述蒸馏系统采用单级蒸馏，仅包含一级蒸馏器，所述蒸馏系统海水输入口、蒸馏系统卤水输出口、蒸馏系统蒸汽输出口、蒸馏系统传热工质输入口、蒸馏系统传热工质输出口均设置在一级蒸馏器上。
可选地，所述蒸馏系统采用两级蒸馏，由一级蒸馏器和二级蒸馏器组成，所述蒸馏系统海水输入口、蒸馏系统传热工质输入口设置在一级蒸馏器上，所述蒸馏系统卤水输出口、蒸馏系统传热工质输出口设置在二级蒸馏器上。所述蒸馏系统蒸汽输出口包括设置在一级蒸馏器上的空调用蒸汽输出口，以及设置在二级蒸馏器上的蒸发蒸汽输出口。所述一级蒸馏器的海水输出口与二级蒸馏器的海水输入口相连，所述一级蒸馏器的传热工质输出口与二级蒸馏器的传热工质输入口相连。所述空调用蒸汽输出口与空调系统加热蒸汽输入口相连，所述蒸发蒸汽输出口与换热系统蒸馏蒸汽输入口相连。
优选地，所述蒸馏系统采用多级蒸馏，其包括至少三个蒸馏器，按照海水流动方向前两个蒸馏器分别为一级蒸馏器、二级蒸馏器，最后一级蒸馏器为末级蒸馏器。所述蒸馏系统海水输入口、蒸馏系统传热工质输入口设置在一级蒸馏器上，所述蒸馏系统传热工质输出口设置在二级蒸馏器上，所述一级蒸馏器的传热工质输出口与二级蒸馏器的传热工质输入口相连。所述蒸馏系统卤水输出口设置在末级蒸馏器上。各级蒸馏器的海水 输出口与下一级蒸馏器的海水输入口相连，二级以后(含二级)、末级之前(不含末级)的各蒸馏器的蒸汽输出口与其下一级的蒸馏器的加热蒸汽输入口相连，通过该级产生的蒸汽对下一级蒸馏器中的海水进行加热。各级蒸馏器内压力逐级降低，因此上一级蒸汽的温度高于下一级蒸馏器内海水的沸点，可以对下一级蒸馏器进行加热。所述蒸馏系统蒸汽输出口包括设置在一级蒸馏器上的空调用蒸汽输出口，设置在二级蒸馏器之后(不含)的各级蒸馏器上的加热蒸汽输出口，以及设置在末级蒸馏器上的蒸发蒸汽输出口。所述空调用蒸汽输出口与空调系统加热蒸汽输入口相连。所述加热蒸汽输出口、蒸发蒸汽输出口与换热系统蒸馏蒸汽输入口相连。
优选地，所述蒸汽冷凝装置包括淡水冷凝器和蒸汽换热器，所述空调冷却装置包括海水冷却换热器，所述卤水换热装置包括卤水冷却换热器。所述淡水冷凝器、海水冷却换热器、卤水冷却换热器和蒸汽换热器的低温侧依次串联连接。所述换热系统海水输入口设置在淡水冷凝器的低温侧输入端，所述换热系统海水输出口设置在蒸汽换热器的低温侧输出端。所述换热系统蒸馏蒸汽输入口设置在淡水冷凝器的高温侧输入端，所述空调返回蒸汽输入口设置在蒸汽换热器的高温侧输入端。所述换热系统卤水输入口、换热系统卤水输出口分别设置在卤水冷却换热器的高温侧的两端。所述换热系统淡水输出口设置在淡水冷凝器和蒸汽换热器的高温侧输出端。所述换热系统空调冷却工质输入口、换热系统空调冷却工质输出口设置在海水冷却换热器高温侧的两端。
优选地，该系统还包括用于收集冷凝水的淡水箱，所述淡水箱上设置有淡水收集口和未凝结蒸汽输出口，所述淡水收集口与换热系统淡水输出口相连。所述未凝结蒸汽输出口与换热系统的蒸汽冷凝装置相连。
优选地，所述吸收式空调系统为单效或多效溴化锂空调。
优选地，所述吸收式空调系统为双效溴化锂空调，所述吸收式空调系统包括高压发生器、低压发生器、冷凝器、蒸发器和吸收器。所述空调系统加热蒸汽输入口和空调系统加热蒸汽输出口设置在高压发生器上，所述高压发生器的溶液输出端与低压发生器的溶液输入端相连。所述高压发生器的一次蒸汽输出端与低压发生器的一次蒸汽输入端相连，所述低压发生器的二次蒸汽输出端与所述冷凝器的二次蒸汽输入端相连，所述低压发生器的一次蒸汽冷凝液输出端与所述冷凝器的一次蒸汽冷凝液输入端相连，所述冷凝器的冷剂输出端与蒸发器的冷剂输入端相连，所述蒸发器的蒸汽输出端与所述吸收器的 蒸汽输入端相连。所述吸收器的溶液输出端与高压发生器的溶液输入端相连，二者之间设置有低温换热器和高温换热器，所述吸收器的溶液输出端、低温换热器的低温侧、高温换热器的低温侧、高压发生器的溶液输入端依次相连。所述高压发生器的溶液输出端、高温换热器的高温侧、低压发生器的溶液输入端依次相连，所述低压发生器的溶液输出端、低温换热器的高温侧、吸收器的溶液输入端依次相连。所述空调系统冷却工质输入口、冷凝器的冷却换热装置、吸收器的冷却换热装置、空调系统冷却工质输出口依次相连。所述蒸发器内设置有冷水换热器，所述冷水换热器的两端分别设置有空调系统冷水输入口和空调系统冷水输出口，所述蒸发器的下部设置有循环冷剂输出端，上部设置有循环冷剂输入端，所述循环冷剂输出端和循环冷剂输入端之间设置有冷剂泵。
优选地，所述所述太阳能集热器与蒸馏系统传热工质输入口之间设置有传热工质循环泵。
优选地，所述太阳能集热器为中高温集热器。
本发明的有益效果是：1)海水淡化利用太阳能加热产生蒸汽，产生的蒸汽作为吸收式空调系统的热源，可充分实现能源的梯级利用，利用效率高；2)吸收式空调系统的冷却工质通过海水进行换热冷却，并对海水进行预热，既节省了吸收式空调系统的冷却用水，又充分回收了吸收式空调系统的余热，从而实现整个系统热效率的大幅提升；3)太阳能属于清洁能源，对环境友好、零排放，采用太阳能驱动的海水淡化与空调联合运行，能够充分利用太阳能，有利于环境保护，具有极大地社会效益、环境效益及经济效益。
附图说明
图1为本发明所设计的高效太阳能海水淡化与空调制冷联合运行系统的工艺流程简图。
图2为图1中太阳能集热系统的结构示意图
图3为图1中吸收式空调系统采用单效加热时的结构示意图
图4为图1中吸收式空调系统采用多效加热时的结构示意图
图5为图1中蒸馏系统采用一级加热时的结构示意图
图6为图1中蒸馏系统采用二级加热时的结构示意图
图7为图1中蒸馏系统采用三级加热时的结构示意图
图8为图1中换热系统的一种结构示意图
图9为图1中换热系统的另一种结构示意图
图10为实施例1的总体结构示意图
其中：高压发生器1、空调系统加热蒸汽输入口1.1、空调系统加热蒸汽输出口1.2、低压发生器2、冷凝器3、空调系统冷却工质输出口3.1、蒸发器4、冷剂泵5、冷水泵6、末端空调设备7、吸收器8、空调系统冷却工质输入口8.1、溶剂泵9、低温换热器10、高温换热器11、蒸汽换热器12、卤水泵13、末级蒸馏器14、二级蒸馏器15、一级蒸馏器16、太阳能集热器17、集热系统传热工质输入口17.1、集热系统传热工质输出口17.2、传热工质循环泵18、淡水冷凝器19、冷却泵20、海水冷却换热器21、海水泵22、淡水泵23、海水增压泵24、淡水箱25、淡水收集口25.1、未凝结蒸汽输出口25.2、卤水冷却换热器26、蒸馏系统27、蒸馏系统海水输入口27.1、蒸馏系统卤水输出口27.2、蒸馏系统蒸汽输出口27.3、空调用蒸汽输出口27.3a、加热蒸汽输出口27.3b、蒸发蒸汽输出口27.3c、蒸馏系统传热工质输入口27.4、蒸馏系统传热工质输出口27.5、换热系统28、换热系统海水输入口28.1、换热系统海水输出口28.2、蒸汽冷凝装置29、换热系统蒸馏蒸汽输入口29.1、蒸馏蒸发蒸汽输入口29.1a、蒸馏冷凝蒸汽输入口29.1b、空调返回蒸汽输入口29.2、换热系统淡水输出口29.3、空调冷却装置30、换热系统空调冷却工质输入口30.1、换热系统空调冷却工质输出口30.2、卤水换热装置31、换热系统卤水输入口31.1、换热系统卤水输出口31.2
具体实施方式
下面结合附图和具体实施例对本发明作进一步的详细说明。
实施例1
如图1所示，本发明所设计的高效太阳能海水淡化与空调制冷联合运行系统，包括太阳能集热系统Ⅰ、海水淡化系统Ⅱ和吸收式空调系统Ⅲ。其中：太阳能集热系统Ⅰ的主要部分为太阳能集热器17，采用中高温集热器。如图2所示，太阳能集热器17设置有集热系统传热工质输入口17.1、集热系统传热工质输出口17.2和传热工质循环泵18。海水淡化系统Ⅱ包括蒸馏系统27和换热系统28。
如图1、图7所示，蒸馏系统27包括三个蒸馏器，按照海水流动方向分别为一级蒸 馏器16、二级蒸馏器15和末级蒸馏器14(本例中为三级蒸馏器)。蒸馏系统27设置有蒸馏系统海水输入口27.1、蒸馏系统卤水输出口27.2、蒸馏系统蒸汽输出口27.3、蒸馏系统传热工质输入口27.4和蒸馏系统传热工质输出口27.5。蒸馏系统海水输入口27.1、蒸馏系统传热工质输入口27.4设置在一级蒸馏器16上，蒸馏系统传热工质输出口27.5设置在二级蒸馏器15上，一级蒸馏器16的传热工质输出口与二级蒸馏器15的传热工质输入口相连。蒸馏系统卤水输出口27.2设置在末级蒸馏器14上。各级蒸馏器的海水输出口与下一级蒸馏器的海水输入口相连，二级蒸馏器15的蒸汽输出口与末级蒸馏器14的加热蒸汽输入口相连，通过二级蒸馏器15产生的蒸汽对末级蒸馏器14中的海水进行加热。蒸馏系统蒸汽输出口27.3包括设置在一级蒸馏器16上的空调用蒸汽输出口27.3a，设置在末级蒸馏器14上的加热蒸汽输出口27.3b，以及蒸发蒸汽输出口27.3c。空调用蒸汽输出口27.3a与空调系统加热蒸汽输入口1.1相连。
如图1、图8所示，换热系统28包括蒸汽冷凝装置29、空调冷却装置30和卤水换热装置31。换热系统28设置有换热系统海水输入口28.1、换热系统海水输出口28.2。蒸汽冷凝装置29设置有换热系统蒸馏蒸汽输入口29.1、空调返回蒸汽输入口29.2和换热系统淡水输出口29.3。空调冷却装置30设置有换热系统空调冷却工质输入口30.1和换热系统空调冷却工质输出口30.2。卤水换热装置31的高温侧设置有换热系统卤水输入口31.1和换热系统卤水输出口31.2，换热系统卤水输入口31.1与蒸馏系统卤水输出口27.2相连。蒸汽冷凝装置29包括淡水冷凝器19和蒸汽换热器12，空调冷却装置30包括海水冷却换热器21，卤水换热装置31包括卤水冷却换热器26。淡水冷凝器19、海水冷却换热器21、卤水冷却换热器26和蒸汽换热器12的低温侧依次串联连接。海水冷却换热器21、卤水冷却换热器26的低温侧之间设置有海水增压泵24。换热系统海水输入口28.1设置在淡水冷凝器19的低温侧输入端，换热系统海水输入口28.1前设置有海水泵22，换热系统海水输出口28.2设置在蒸汽换热器12的低温侧输出端。换热系统蒸馏蒸汽输入口29.1包括蒸馏蒸发蒸汽输入口29.1a和蒸馏冷凝蒸汽输入口29.1b，其中，蒸馏蒸发蒸汽输入口29.1a设置在淡水冷凝器19的高温侧输入端，蒸馏冷凝蒸汽输入口29.1b与淡水箱25相连；空调返回蒸汽输入口29.2设置在蒸汽换热器12的高温侧输入端。换热系统卤水输入口31.1、换热系统卤水输出口31.2分别设置在卤水冷却换热器26的高温侧的两端，换热系统卤水输入口31.1附近设置有卤水泵13。换热系统淡水输出口 29.3设置在淡水冷凝器19和蒸汽换热器12的高温侧输出端。换热系统空调冷却工质输入口30.1、换热系统空调冷却工质输出口30.2设置在海水冷却换热器21高温侧的两端，换热系统空调冷却工质输出口30.2附近设置有冷却泵20。淡水箱25上设置有淡水收集口25.1和未凝结蒸汽输出口25.2，淡水箱25的淡水输出口上设置有淡水泵23。蒸汽换热器12的高温侧、换热系统淡水输出口29.3和蒸馏冷凝蒸汽输入口29.1b分别与淡水收集口25.1相连。未凝结蒸汽输出口25.2与淡水冷凝器19相连。
如图1、图4所示，本实施例中，吸收式空调系统Ⅲ为双效溴化锂空调，吸收式空调系统Ⅲ包括高压发生器1、低压发生器2、冷凝器3、蒸发器4和吸收器8。高压发生器1上设置有空调系统加热蒸汽输入口1.1和空调系统加热蒸汽输出口1.2，高压发生器1的溶液输出端与低压发生器2的溶液输入端相连。高压发生器1的一次蒸汽输出端与低压发生器2的一次蒸汽输入端相连，低压发生器2的二次蒸汽输出端与冷凝器3的二次蒸汽输入端相连，低压发生器2的一次蒸汽冷凝液输出端与冷凝器3的一次蒸汽冷凝液输入端相连，冷凝器3的冷剂输出端与蒸发器4的冷剂输入端相连，蒸发器4的蒸汽输出端与吸收器8的蒸汽输入端相连。吸收器8的溶液输出端与高压发生器1的溶液输入端相连，二者之间设置有低温换热器10和高温换热器11，吸收器8的溶液输出端、低温换热器10的低温侧、高温换热器11的低温侧、高压发生器1的溶液输入端依次相连，吸收器8中的溴化锂溶液通过溶剂泵9输送到高压发生器1中。高压发生器1的溶液输出端、高温换热器11的高温侧、低压发生器2的溶液输入端依次相连，低压发生器2的溶液输出端、低温换热器10的高温侧、吸收器8的溶液输入端依次相连。空调系统冷却工质输入口8.1、冷凝器3的冷却换热装置、吸收器8的冷却换热装置、空调系统冷却工质输出口3.1依次相连。蒸发器4内设置有冷水换热器，冷水换热器的两端分别设置有空调系统冷水输入口和空调系统冷水输出口，二者分别与末端空调设备7上的冷水输出口和冷水输入口相连，其中的低温冷水通过冷水泵6进行循环。蒸发器4的下部设置有循环冷剂输出端，上部设置有循环冷剂输入端，循环冷剂输出端和循环冷剂输入端之间设置有冷剂泵5。
如图1、图4、图7、图9、图10所示，各系统输入输出口的连接关系如下：集热系统传热工质输入口17.1与蒸馏系统传热工质输出口27.5相连，集热系统传热工质输出口17.2与蒸馏系统传热工质输入口27.4相连。蒸馏系统海水输入口27.1与换热系统海水输 出口28.2相连。空调系统加热蒸汽输入口1.1与空调用蒸汽输出口27.3a相连，空调系统加热蒸汽输出口1.2与空调返回蒸汽输入口29.2相连。蒸馏蒸发蒸汽输入口29.1a、蒸馏冷凝蒸汽输入口29.1b分别与蒸发蒸汽输出口27.3c、加热蒸汽输出口27.3b相连。换热系统空调冷却工质输入口30.1与空调系统冷却工质输出口3.1相连，换热系统空调冷却工质输出口30.2与空调系统冷却工质输入口8.1相连。
上述装置的工作流程简述如下：
太阳能集热器17通过光热转化吸收太阳能传递给导热工质(本例中为导热油)，导热工质依次流入一级蒸馏器16和二级蒸馏器15，通过设置在两蒸馏器内部的换热器为淡化海水提供所需热量，导热工质从二级蒸馏器15流出后经传热工质循环泵18流回太阳能集热器17。
海水经海水泵22流入淡水冷凝器19，为蒸汽冷凝提供冷源；海水由淡水冷凝器19流出后，部分直接排空，部分依次流入海水冷却换热器21、卤水换热器26、蒸汽换热器12，分别对吸收式空调系统Ⅲ、卤水、空调返回蒸汽进行余热回收；经预热后的海水流入一级蒸馏器16蒸馏，蒸馏后的浓海水依次流入二级蒸馏器15、末级蒸馏器16中继续蒸馏，最后经卤水泵13流入卤水换热器26将余热传递给海水；一级蒸馏器16蒸馏出的蒸汽直接作为吸收式空调系统Ⅲ的热源；二级蒸馏器15蒸馏出的蒸汽进入末级蒸馏器14内通过其内的换热器将热量传递给浓海水，经末级蒸馏器14冷凝的蒸汽流入淡水箱25，部分未冷凝的蒸汽由淡水箱25的未凝结蒸汽输出口25.2进入淡水冷凝器19内进一步冷凝；末级蒸馏器14蒸馏出的蒸汽进入淡水冷凝器19将热量传递给海水，冷凝后的淡水从淡水收集口25.1流入淡水箱25，淡水箱25内的淡水经淡水泵23供应至淡水需求端。
一级蒸馏器16蒸馏出的蒸汽输入高压发生器1内作为吸收式空调系统Ⅲ的热源，通过其内的换热器将热量传递给高压发生器1内的溴化锂水溶液后，经蒸汽换热器12与海水换热后进入淡水箱25内。溴化锂水溶液在高压发生器1内经其内的换热器加热蒸发出水蒸气后，溶液经过高温换热器11进入低压发生器2内经其内的换热器加热继续蒸发出水蒸气，二次蒸发后的溴化锂水溶液流出低压发生器2，再经低温换热器10流入吸收器8。溴化锂水溶液在吸收器8内与低温低压水蒸气溶解再生，再生过程中放出的热量通过其内的换热器移出。吸收器8内经过再生的溴化锂水溶液经溶剂泵9增压后依次流入低 温换热器10、高温换热器11进行换热升温，最后进入高压发生器1内。高压发生器1内蒸发出的水蒸气进入低压发生器2内，通过低压发生器2内的换热器将热量传递给低压发生器2内的溴化锂水溶液，回收其中的热能，加热后的水蒸气凝结成水流入冷凝器3内，低压发生器2内经加热蒸发产生的蒸汽也进入冷凝器3内进行冷凝。冷凝器3内收集的冷剂水通过其内的换热器降温后流入蒸发器4内。蒸发器4内属于低温真空环境，其内的冷剂水经冷剂泵5增压喷淋回蒸发器4内，水在喷回蒸发器4内瞬间压力巨变汽化，在水汽化过程中从换热器内吸收热量，低温低压水蒸气被吸收器8内的溴化锂水溶液吸收。传热工质(本例中为水)经冷水泵6流入蒸发器4内，通过蒸发器4内的换热器吸收冷量后流入末端空调设备7，由末端空调设备7为用户供冷。冷却工质经冷却泵20依次流入吸收器8、冷凝器3通过各自内部的换热器分别为溴化锂水溶液、水降温后，流入海水冷却换热器21，将热量传递给海水侧后流入冷却泵20，形成循环。
实施例2
本实施例中，总体结构与实施例1类似，不同之处在于：
如图5所示，蒸馏系统27仅包含一级蒸馏器16，蒸馏系统海水输入口27.1、蒸馏系统卤水输出口27.2、蒸馏系统蒸汽输出口27.3、蒸馏系统传热工质输入口27.4、蒸馏系统传热工质输出口27.5均设置在一级蒸馏器16上。一级蒸馏器16经传热工质加热产生的蒸汽一部分输入吸收式空调系统Ⅲ中作为热源，另一部分输入蒸汽冷凝装置29进行冷凝。
如图3所示，吸收式空调系统Ⅲ为单效溴化锂空调，与双效溴化锂空调的不同之处在于，该空调系统的发生器只有一个(图中沿用高压发生器的编号1)。
实施例3
本实施例中，总体结构与实施例1类似，不同之处在于：
如图6所示，蒸馏系统27由一级蒸馏器16和二级蒸馏器15组成，蒸馏系统海水输入口27.1、蒸馏系统传热工质输入口27.4设置在一级蒸馏器16上，蒸馏系统卤水输出口27.2、蒸馏系统传热工质输出口27.5设置在二级蒸馏器15上。蒸馏系统蒸汽输出口27.3包括设置在一级蒸馏器16上的空调用蒸汽输出口27.3a，以及设置在二级蒸馏器15上的蒸发蒸汽输出口27.3c。一级蒸馏器16的海水输出口与二级蒸馏器15的海水输入口相连，一级蒸馏器16的传热工质输出口与二级蒸馏器15的传热工质输入口相连。空调 用蒸汽输出口27.3a与空调系统加热蒸汽输入口1.1相连，蒸发蒸汽输出口27.3c与换热系统蒸馏蒸汽输入口29.1相连。
如图9所示，换热系统(28)未设置蒸汽换热器(12)，空调返回蒸汽输入口(29.2)设置在淡水冷凝器(19)上，即空调加热后的返回蒸汽直接通入淡水冷凝器(19)进行冷却。

Claims (13)

  1. 一种高效太阳能海水淡化与空调制冷联合运行方法，包括太阳能集热步骤、海水淡化步骤和空调制冷步骤，其特征在于：
    所述太阳能集热步骤中，对太阳能进行光热转换，所产生的热量传递给传热工质；
    所述海水淡化步骤中，以所述太阳能集热步骤获得的传热工质作为热源对海水进行加热蒸馏，所得蒸馏蒸汽再与海水换热后冷凝得到淡水；
    所述空调制冷步骤中，将所述海水淡化步骤获得的蒸馏蒸汽输送到吸收式空调系统，作为热源蒸汽对制冷工质对进行加热；该蒸馏蒸汽将热量传递给制冷工质对后，再返回所述海水淡化步骤中，进一步与海水换热冷凝得到淡水，同时对海水进行预热；
    所述吸收式空调系统通过冷却工质循环吸收在制冷过程中释放的热量，吸收热量后温度升高的冷却工质与所述海水淡化步骤中的海水进行换热，将其中的热量转移到海水中，使所述冷却工质得到冷却，并对海水进行预热。
  2. 根据权利要求1所述的高效太阳能海水淡化与空调制冷联合运行方法，其特征在于：所述海水淡化步骤中，采用多级蒸馏器串联的方式进行蒸馏，海水依次通过一级蒸馏器(16)、二级蒸馏器(15)及其后的各级蒸馏器；在一级蒸馏器(16)、二级蒸馏器(15)中通过所述太阳能集热步骤获得的传热工质对海水进行加热，一级蒸馏器(16)产生的蒸汽通入所述吸收式空调系统中作为热源蒸汽，二级以后、末级之前的各级蒸馏器产生的蒸汽通入下一级蒸馏器中对海水进行加热，加热后部分冷凝的蒸汽及末级蒸馏器(14)蒸发产生的蒸汽再与海水换热后冷凝得到淡水。
  3. 一种为实现权利要求1所述方法而设计的高效太阳能海水淡化与空调制冷联合运行系统，包括太阳能集热系统(Ⅰ)、海水淡化系统(Ⅱ)和吸收式空调系统(Ⅲ)，其特征在于：
    所述太阳能集热系统(Ⅰ)包括太阳能集热器(17)，所述太阳能集热器(17)设置有集热系统传热工质输入口(17.1)和集热系统传热工质输出口(17.2)；
    所述海水淡化系统(Ⅱ)包括蒸馏系统(27)和换热系统(28)；
    所述蒸馏系统(27)包括至少一个蒸馏器，所述蒸馏系统(27)设置有蒸馏系统海水输入口(27.1)、蒸馏系统卤水输出口(27.2)、蒸馏系统蒸汽输出口(27.3)、蒸馏系统传热工质输入口(27.4)和蒸馏系统传热工质输出口(27.5)；
    所述换热系统(28)包括蒸汽冷凝装置(29)和空调冷却装置(30)；所述换热系统(28)设置有换热系统海水输入口(28.1)、换热系统海水输出口(28.2)；所述蒸汽冷凝装置(29)设置有换热系统蒸馏蒸汽输入口(29.1)、空调返回蒸汽输入口(29.2)、换热系统淡水输出口(29.3)；所述空调冷却装置(30)设置有换热系统空调冷却工质输入口(30.1)和换热系统空调冷却工质输出口(30.2)；
    所述换热系统蒸馏蒸汽输入口(29.1)、空调返回蒸汽输入口(29.2)设置在蒸汽冷凝装置(29)的高温侧入口，所述换热系统淡水输出口(29.3)设置在蒸汽冷凝装置(29)的高温侧出口，所述换热系统空调冷却工质输入口(30.1)和换热系统空调冷却工质输出口(30.2)设置在空调冷却装置(30)的高温侧两端；所述蒸汽冷凝装置(29)的低温侧两端、空调冷却装置(30)的低温侧两端分别设置有海水输入口和海水输出口；
    所述吸收式空调系统(Ⅲ)包括空调系统加热蒸汽输入口(1.1)、空调系统加热蒸汽输出口(1.2)、空调系统冷却工质输入口(8.1)和空调系统冷却工质输出口(3.1)；
    所述集热系统传热工质输入口(17.1)与蒸馏系统传热工质输出口(27.5)相连，所述集热系统传热工质输出口(17.2)与蒸馏系统传热工质输入口(27.4)相连；所述蒸馏系统海水输入口(27.1)与换热系统海水输出口(28.2)相连；所述空调系统加热蒸汽输入口(1.1)、换热系统蒸馏蒸汽输入口(29.1)分别与蒸馏系统蒸汽输出口(27.3)相连，所述空调系统加热蒸汽输出口(1.2)与空调返回蒸汽输入口(29.2)相连；所述换热系统空调冷却工质输入口(30.1)与空调系统冷却工质输出口(3.1)相连，所述换热系统空调冷却工质输出口(30.2)与空调系统冷却工质输入口(8.1)相连。
  4. 根据权利要求3所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述换热系统(28)还设置有利用蒸馏得到的卤水对海水进行预热的卤水换热装置(31)，所述卤水换热装置(31)的高温侧设置有换热系统卤水输入口(31.1)和换热系统卤水输出口(31.2)，所述卤水换热装置(31)的低温侧设置有海水输入口和海水输出口，所述换热系统卤水输入口(31.1)与蒸馏系统卤水输出口(27.2)相连。
  5. 根据权利要求3所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述蒸馏系统(27)仅包含一级蒸馏器(16)，所述蒸馏系统海水输入口(27.1)、蒸馏系统卤水输出口(27.2)、蒸馏系统蒸汽输出口(27.3)、蒸馏系统传热工质输入口(27.4)、蒸馏系统传热工质输出口(27.5)均设置在一级蒸馏器(16)上。
  6. 根据权利要求3所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述蒸馏系统(27)由一级蒸馏器(16)和二级蒸馏器(15)组成，所述蒸馏系统海水输入口(27.1)、蒸馏系统传热工质输入口(27.4)设置在一级蒸馏器(16)上，所述蒸馏系统卤水输出口(27.2)、蒸馏系统传热工质输出口(27.5)设置在二级蒸馏器(15)上；所述蒸馏系统蒸汽输出口(27.3)包括设置在一级蒸馏器(16)上的空调用蒸汽输出口(27.3a)，以及设置在二级蒸馏器(15)上的蒸发蒸汽输出口(27.3c)；所述一级蒸馏器(16)的海水输出口与二级蒸馏器(15)的海水输入口相连，所述一级蒸馏器(16)的传热工质输出口与二级蒸馏器(15)的传热工质输入口相连；所述空调用蒸汽输出口(27.3a)与空调系统加热蒸汽输入口(1.1)相连，所述蒸发蒸汽输出口(27.3c)与换热系统蒸馏蒸汽输入口(29.1)相连。
  7. 根据权利要求3所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述蒸馏系统(27)包括至少三个蒸馏器，按照海水流动方向前两个蒸馏器分别为一级蒸馏器(16)、二级蒸馏器(15)，最后一级蒸馏器为末级蒸馏器(14)；所述蒸馏系统海水输入口(27.1)、蒸馏系统传热工质输入口(27.4)设置在一级蒸馏器(16)上，所述蒸馏系统传热工质输出口(27.5)设置在二级蒸馏器(15)上，所述一级蒸馏器(16)的传热工质输出口与二级蒸馏器(15)的传热工质输入口相连；所述蒸馏系统卤水输出口(27.2)设置在末级蒸馏器(14)上；各级蒸馏器的海水输出口与下一级蒸馏器的海水输入口相连，二级以后、末级之前的各蒸馏器的蒸汽输出口与其下一级的蒸馏器的加热蒸汽输入口相连，通过该级产生的蒸汽对下一级蒸馏器中的海水进行加热；所述蒸馏系统蒸汽输出口(27.3)包括设置在一级蒸馏器(16)上的空调用蒸汽输出口(27.3a)，设置在二级蒸馏器(15)之后的各级蒸馏器上的加热蒸汽输出口(27.3b)，以及设置在末级蒸馏器(14)上的蒸发蒸汽输出口(27.3c)；所述空调用蒸汽输出口(27.3a)与空 调系统加热蒸汽输入口(1.1)相连；所述加热蒸汽输出口(27.3b)、蒸发蒸汽输出口(27.3c)与换热系统蒸馏蒸汽输入口(29.1)相连。
  8. 根据权利要求4所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述蒸汽冷凝装置(29)包括淡水冷凝器(19)和蒸汽换热器(12)，所述空调冷却装置(30)包括海水冷却换热器(21)，所述卤水换热装置(31)包括卤水冷却换热器(26)；所述淡水冷凝器(19)、海水冷却换热器(21)、卤水冷却换热器(26)和蒸汽换热器(12)的低温侧依次串联连接；所述换热系统海水输入口(28.1)设置在淡水冷凝器(19)的低温侧输入端，所述换热系统海水输出口(28.2)设置在蒸汽换热器(12)的低温侧输出端；所述换热系统蒸馏蒸汽输入口(29.1)设置在淡水冷凝器(19)的高温侧输入端，所述空调返回蒸汽输入口(29.2)设置在蒸汽换热器(12)的高温侧输入端；所述换热系统卤水输入口(31.1)、换热系统卤水输出口(31.2)分别设置在卤水冷却换热器(26)的高温侧的两端；所述换热系统淡水输出口(29.3)设置在淡水冷凝器(19)和蒸汽换热器(12)的高温侧输出端；所述换热系统空调冷却工质输入口(30.1)、换热系统空调冷却工质输出口(30.2)设置在海水冷却换热器(21)高温侧的两端。
  9. 根据权利要求3所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：该系统还包括用于收集冷凝水的淡水箱(25)，所述淡水箱(25)上设置有淡水收集口(25.1)和未凝结蒸汽输出口(25.2)，所述淡水收集口(25.1)与换热系统淡水输出口(29.3)相连；所述未凝结蒸汽输出口(25.2)与换热系统(28)的蒸汽冷凝装置(29)相连。
  10. 根据权利要求3～9中任一项所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述吸收式空调系统(Ⅲ)为单效或多效溴化锂空调。
  11. 根据权利要求10所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述吸收式空调系统(Ⅲ)为双效溴化锂空调，所述吸收式空调系统(Ⅲ)包括高压发生器(1)、低压发生器(2)、冷凝器(3)、蒸发器(4)和吸收器(8)；所述空调 系统加热蒸汽输入口(1.1)和空调系统加热蒸汽输出口(1.2)设置在高压发生器(1)上，所述高压发生器(1)的溶液输出端与低压发生器(2)的溶液输入端相连；所述高压发生器(1)的一次蒸汽输出端与低压发生器(2)的一次蒸汽输入端相连，所述低压发生器(2)的二次蒸汽输出端与所述冷凝器(3)的二次蒸汽输入端相连，所述低压发生器(2)的一次蒸汽冷凝液输出端与所述冷凝器(3)的一次蒸汽冷凝液输入端相连，所述冷凝器(3)的冷剂输出端与蒸发器(4)的冷剂输入端相连，所述蒸发器(4)的蒸汽输出端与所述吸收器(8)的蒸汽输入端相连；所述吸收器(8)的溶液输出端与高压发生器(1)的溶液输入端相连，二者之间设置有低温换热器(10)和高温换热器(11)，所述吸收器(8)的溶液输出端、低温换热器(10)的低温侧、高温换热器(11)的低温侧、高压发生器(1)的溶液输入端依次相连；所述高压发生器(1)的溶液输出端、高温换热器(11)的高温侧、低压发生器(2)的溶液输入端依次相连，所述低压发生器(2)的溶液输出端、低温换热器(10)的高温侧、吸收器(8)的溶液输入端依次相连；所述空调系统冷却工质输入口(8.1)、冷凝器(3)的冷却换热装置、吸收器(8)的冷却换热装置、空调系统冷却工质输出口(3.1)依次相连；所述蒸发器(4)内设置有冷水换热器，所述冷水换热器的两端分别设置有空调系统冷水输入口和空调系统冷水输出口，所述蒸发器(4)的下部设置有循环冷剂输出端，上部设置有循环冷剂输入端，所述循环冷剂输出端和循环冷剂输入端之间设置有冷剂泵(5)。
  12. 根据权利要求3～9中任一项所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述太阳能集热器(17)与蒸馏系统传热工质输入口(27.4)之间设置有传热工质循环泵(18)。
  13. 根据权利要求3～9中任一项所述的高效太阳能海水淡化与空调制冷联合运行系统，其特征在于：所述太阳能集热器(17)为中高温集热器。
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