WO2023036066A1 - 高效率的真空升华蒸发冷热能分离系统和分离方法及其应用 - Google Patents

高效率的真空升华蒸发冷热能分离系统和分离方法及其应用 Download PDF

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WO2023036066A1
WO2023036066A1 PCT/CN2022/116936 CN2022116936W WO2023036066A1 WO 2023036066 A1 WO2023036066 A1 WO 2023036066A1 CN 2022116936 W CN2022116936 W CN 2022116936W WO 2023036066 A1 WO2023036066 A1 WO 2023036066A1
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compressor
steam
outlet
condenser
working medium
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PCT/CN2022/116936
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English (en)
French (fr)
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武伟
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武伟
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
    • F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
    • F01D15/10—Adaptations for driving, or combinations with, electric generators
    • 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
    • F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
    • F22B3/04—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass by drop in pressure of high-pressure hot water within pressure- reducing chambers, e.g. in accumulators
    • 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

Definitions

  • the invention belongs to the technical field of green energy, relates to a vacuum sublimation evaporation cold-heat energy separation system, in particular provides a high-efficiency vacuum sublimation evaporation cold-heat energy separation system, and also provides a separation method using the separation system.
  • the application of the separation system in ocean temperature difference power generation is also provided.
  • Vacuum sublimation evaporation cold heat energy separation technology is a technology that uses vacuum evaporation and sublimation to separate water energy.
  • Water contains a lot of energy, and the latent heat of crystallization released by freezing one ton of 0°C water into ice can heat one ton of 20°C normal temperature water to 100°C, and the energy can reach 93KWH.
  • the potential energy of one ton of water can only generate about 0.3KWH, which is only 0.32% of the latent heat energy of crystallization in one ton of water, that is, the latent heat of crystallization in the same amount of water is equal to the drop of 100 meters of water.
  • the Three Gorges Dam generates about 100 billion kilowatt-hours of electricity every year, and the flow of the Yangtze River is nearly 1 trillion tons per year. (my country's annual power generation capacity is 7,225.5 billion kWh, and civilian electricity is 1,024.8 billion kWh. Calculation shows that the power generation of the Three Gorges is 1.38% of the total power generation in the country).
  • the latent heat of crystallization contained in the water volume of this basin is about 93 trillion degrees. The power generation is only about one-thousandth of the latent heat of crystallization contained.
  • the separated energy allows heat energy to be stored in the form of hot water or steam, and cold energy to be stored in the form of ice slurry or ice cubes and utilized.
  • Hot water at 35-40 degrees can be used for heating in winter, planting and breeding in agricultural greenhouses and other production activities. Even in winter in northern my country, the flowing water under the ice layer of the river still retains huge energy.
  • the ice after separating the heat energy can be melted naturally under the appropriate season or condition. It can provide a new production model for vast areas with a short frost-free period.
  • the separated cold energy can be used for production activities such as ice making, air conditioning in summer (underground cooling, 16-18 degrees cold water can be realized), and cold source for agricultural product preservation.
  • the freezing method can also be used for desalination of seawater and brackish water to open up new water sources.
  • the cold and heat energy separation technology is a green energy technology with a wide range of uses and great development prospects.
  • the proposal of ocean temperature difference power generation is based on the phenomenon that there is a temperature difference of about 20°C between the surface of seawater and the depth. Only the sensible heat in seawater is used to generate power, so that the heat energy used per ton of water is insufficient, resulting in low power generation efficiency, requiring a large amount of seawater, and the extraction of deep seawater consumes a lot of energy.
  • the separation of cold and heat energy is to utilize the latent heat of the liquid, which is bound to greatly improve the power generation efficiency and reduce the water delivery volume compared with only using the sensible heat of the liquid. There is no such solution in the prior art.
  • the cold and heat energy separation system includes a sealed container 1 and a vacuum system 2 to vacuum the container 1 to form an artificial environment in which water can evaporate in a vacuum.
  • a vacuum environment 500 Pa
  • the density of water vapor is greatly reduced, which is about 1/200 of that under atmospheric pressure conditions.
  • the mass flow rate will be very small, thus making the separation efficiency not high.
  • the purpose of the present invention is to provide a high-efficiency vacuum sublimation evaporation cooling and heat energy separation system, wherein the vacuum system can pump water vapor generated by vacuum evaporation in a container with a large flow rate to improve the separation efficiency of cold and heat energy.
  • Another object of the present invention is to provide a separation method using the separation system.
  • Another object of the present invention is to provide a system and method for generating electricity using the above-mentioned high-efficiency vacuum sublimation evaporation cold-heat energy separation system.
  • a high-efficiency vacuum sublimation evaporation cold-heat energy separation system includes a sealed container, which is provided with a liquid inlet, a gas outlet, and a solid or solid-liquid mixture outlet; a vacuum system is connected to the gas outlet, It is a vacuum sublimation evaporation unit, which continuously and efficiently extracts the steam in the container to provide a set evaporation pressure for the sealed container;
  • the vacuum sublimation evaporation unit is a compressor unit, which includes at least one compressor.
  • the compressor is provided with a suction port and an exhaust port.
  • the suction port of the compressor is connected to the gas outlet of the container.
  • the compressor unit includes at least two compressors, and each compressor is connected in series.
  • the compressor may be an axial compressor or a centrifugal compressor.
  • the axial flow compressor is a multi-stage axial flow compressor.
  • the multi-stage axial flow compressor includes a casing, and the motor of the compressor is arranged in the casing, and the motor is its two ends.
  • a dual-axis motor with one output shaft and two coaxial shafts is provided, a number of rotor blades are respectively fixed on the two output shafts, and stator blades are arranged between adjacent rotor blades, and the stator blades are fixed on the on the chassis.
  • the same number of rotor blades are arranged symmetrically on the two output shafts.
  • each output shaft Preferably, 2-4 rotor blades are arranged on each output shaft.
  • the ends of the hubs of the rotor blades adjacent to the motor on both sides of the motor are recessed, at least a part of both ends of the motor body is accommodated in the recessed space, and the two rotor blades adjacent to the motor Static blades are arranged on the motor body between them.
  • a cooling device is provided on the body of the motor where the stator vanes are arranged, so as to facilitate heat dissipation of the motor.
  • the stator vane becomes the bracket of the motor in the casing.
  • the power supply input port and the input and output ports of the cooling device are arranged on the bracket.
  • the casing of the multi-stage axial flow compressor is composed of a section of conical barrel and a section of cylindrical barrel, and the end of the large diameter of the conical barrel is the inlet end of the compressor.
  • the multi-stage axial flow compressor is a counter-rotary compressor, that is, it includes two multi-stage axial flow compressors, the casings of the two compressors are sealed, and the two multi-stage axial flow compressors
  • the rotation direction of the impeller is opposite, and the rotation direction of the motor is opposite, forming a counterrotation effect.
  • the vacuum sublimation evaporator unit also includes a heat exchanger as a cooler and/or a condenser, wherein a steam channel and a coolant channel are arranged, and the inlet of the steam channel is connected to the exhaust gas of the previous compressor. port to cool or condense the steam extracted from the compressor.
  • a heat exchanger as a cooler and/or a condenser, wherein a steam channel and a coolant channel are arranged, and the inlet of the steam channel is connected to the exhaust gas of the previous compressor. port to cool or condense the steam extracted from the compressor.
  • the vacuum sublimation evaporation unit further includes a vacuum pump, the outlet of the vacuum pump communicates with the atmosphere, and the inlet of the vacuum pump is connected to the preceding compressor heat exchanger.
  • Scheme 1 comprising a multistage axial flow compressor and a vacuum pump, which are connected in series, the air inlet of the multistage axial flow compressor is connected to the gas outlet of the container, and the air outlet of the vacuum pump is connected to the gas outlet of the container. Atmospheric connectivity.
  • Scheme 2 including a multi-stage axial flow compressor with a counter-rotating structure, a condenser and a vacuum pump, which are connected in series in sequence, and the air inlet of the multi-stage axial flow compressor is connected to the container Gas outlet, the gas outlet of the vacuum pump communicates with the atmosphere.
  • Scheme 3 It includes a counter-rotating multi-stage axial flow compressor and a centrifugal compressor, which are connected in series.
  • Scheme 4 Including a counter-rotating multi-stage axial flow compressor, a cooler, a compressor, a condenser and a vacuum pump, which are connected in series in sequence, and the compressor is a counter-rotating structure Multi-stage axial flow compressor or centrifugal compressor.
  • the vacuum sublimation evaporation unit is more than two axial flow compressors, and also includes a set of gas-liquid heat exchangers, that is, condensers, and the gas-liquid heat exchangers are provided with an air inlet and an air outlet and a liquid discharge port, the air inlet is connected to the exhaust port of the first compressor, the gas outlet is connected to the air inlet of the second compressor, and the gas outlet on the second compressor is The exhaust port communicates with the atmosphere; the liquid discharge port is connected to the pipeline system to collect hot water for utilization.
  • a set of gas-liquid heat exchangers that is, condensers
  • the gas-liquid heat exchangers are provided with an air inlet and an air outlet and a liquid discharge port
  • the axial flow compressor or centrifugal compressor is used as the water vapor extraction device at the outlet of the vacuum environment.
  • the extracted water vapor is compressed and boosted and then passed into the series heat exchanger.
  • the functional requirement of such a heat exchanger has also changed from simple cooling down to being able to condense about 70%-90% of the extracted water vapor, and directly generate condensed water at a certain temperature. In order to obtain a better thermal energy separation effect.
  • the improved primary compressor and the centrifugal compressor form a compressor unit.
  • the vacuum sublimation evaporation unit also includes a set of gas-liquid heat exchangers, namely a condenser and a vacuum pump, and the condenser includes a shell on which an air inlet, an air outlet, and a liquid discharge
  • the air inlet is connected to the exhaust port of the compressor
  • the air outlet is connected to the air inlet of the vacuum pump
  • the exhaust port on the vacuum pump communicates with the atmosphere.
  • the vacuum pump is a screw vacuum pump.
  • the vacuum sublimation evaporation cold-heat energy separation method using the separation system provided by the present invention includes the step of using the vacuum sublimation evaporation unit to extract steam from the container.
  • the steam extracted from the previous compressor is introduced into a heat exchanger before entering the next compressor, as a cooler or condenser, in which the steam extracted from the previous compressor is The steam cools down, and in this condenser, 70-90% of the steam is condensed.
  • the pressure ratio of each compressor in the vacuum sublimation evaporation unit is in the range of 2-20.
  • the pressure ratio of the first stage compressor is 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, and the temperature is 40.5°C. Then, the steam enters the series heat exchanger to condense 70%-90% of the water vapor It is warm water, and then enters the second-stage compressor with a pressure ratio of 15 to extract the remaining water vapor.
  • the pressure ratio of the first stage compressor is 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, and the temperature of 40.5°C. Then, the steam enters the series heat exchanger to condense 70%-90% of the water vapor into Warm water, the remaining water vapor is drawn out from the outlet of the condenser by the screw vacuum pump connected in series behind.
  • the pressure ratio of the first-stage compressor is 4, and then the heat exchanger is connected in series to cool down, and then a centrifugal compressor is connected in series, the pressure ratio is 4, the total pressure ratio is 16, and the corresponding gas-liquid equilibrium pressure is 7500Pa-8000Pa , the temperature is 40.5°C, and then the steam enters the series heat exchanger to condense 70%-90% of the water vapor into warm water, and the remaining water vapor is drawn out from the outlet of the condenser by the screw vacuum pump connected in series behind.
  • the pressure ratio of the first stage compressor: 3-4 corresponding to the gas-liquid equilibrium pressure 1500Pa-2000Pa, temperature 13°-17°C, then the steam enters the series condenser, the input cooling medium temperature is below 2°C, and 40%-90%
  • the water vapor is condensed into warm water, and the remaining water vapor is extracted from the outlet of the condenser by the compressor and/or screw vacuum pump connected in series.
  • the method is suitable for applications where seawater desalination production is the main focus.
  • the coolant in the cooler and/or condenser is air or water at normal temperature, such as air or water at 20-30°C.
  • the coolant in the cooler and/or condenser may be condensed water discharged from the subsequent condenser.
  • the condenser uses the condenser to condense 70%-90% of the water vapor extracted from the compressor into crystal water (above 50 degrees), which is output as heat energy. Since the steam pressures and condensing temperatures output by compressor units with different pressure ratios are different, the present invention provides multiple possibilities for improving process design and obtaining high-efficiency energy separation.
  • the power generation system includes a screw expander or steam turbine, a generator, and the screw expander or steam turbine is provided with a live steam An inlet and a exhaust steam outlet, the shaft of the screw expander or steam turbine is connected to the rotor of the generator, and the feature is: the steam in the vacuum sublimation evaporation unit is passed into the screw expander or steam turbine.
  • the power generation system includes a screw expander or a steam turbine and a generator, and the screw expander or steam turbine is provided with a working medium fresh steam inlet and a working medium exhaust steam outlet, and the screw expander or steam turbine
  • the rotor of the generator connected on the shaft also includes a working fluid evaporator and a working fluid condenser, the working fluid evaporator is provided with a phase change working fluid flow channel and a heating agent flow channel, and the working fluid evaporator
  • the two ends of the phase-change working medium flow channel are the liquid working medium inlet and the gaseous working medium steam outlet respectively.
  • the working medium condenser is provided with a phase-change working medium flow channel and a coolant flow channel.
  • the two ends of the phase-change working medium flow channel are the exhaust steam inlet of the working medium and the outlet of the liquid working medium respectively, and the gaseous working medium steam outlet of the working medium evaporator is connected to the working medium fresh steam inlet of the screw expander or steam turbine,
  • the exhaust steam outlet of the screw expander or steam turbine is connected to the exhaust steam inlet of the working fluid condenser, and the liquid working fluid outlet of the working fluid condenser is connected to the liquid working fluid inlet of the working fluid evaporator;
  • the steam or hot water in the vacuum sublimation evaporation unit is fed into the heating agent channel of the working medium evaporator to heat the working medium into steam and pass it into the screw expander or steam turbine.
  • the working fluid evaporator and the condenser or cooler in the vacuum sublimation evaporation unit are combined into one, and the steam or hot water discharged from the compressor heats the working fluid and then discharges it.
  • the coolant channel in the working fluid condenser directly or indirectly introduces the ice slurry discharged from the container.
  • the above power generation system is:
  • the screw expander or steam turbine includes a screw expander or steam turbine and a generator, the screw expander or steam turbine is provided with a new steam inlet and a exhaust steam outlet, the screw expander or steam turbine is connected to the rotor of the generator on the shaft, the The steam outlet of the compressor unit in the vacuum sublimation evaporation unit is connected to the fresh steam inlet of the screw expander or steam turbine. or,
  • It includes a screw expander or steam turbine and a generator, the screw expander or steam turbine is provided with a fresh steam inlet and a exhaust steam outlet, the shaft of the screw expander or steam turbine is connected with the rotor of the generator, and It includes a working fluid evaporator and a working fluid condenser, the working fluid evaporator is provided with a phase-change working fluid channel and a heating agent channel, and the two ends of the phase-change working fluid channel in the working fluid evaporator are respectively It is the liquid working medium inlet and the new gaseous working medium steam outlet.
  • the working medium condenser is provided with a phase change working medium flow channel and a coolant flow channel.
  • the two ends of the phase change working medium flow channel in the working medium condenser are respectively It is the exhaust steam inlet of the working fluid and the outlet of the new liquid working fluid, the new gaseous working fluid steam outlet of the working fluid evaporator is connected to the steam inlet of the steam turbine, and the exhaust steam outlet of the steam turbine is connected to the working fluid condenser
  • the exhaust steam inlet, the new liquid working fluid outlet of the working fluid condenser is connected to the liquid working fluid inlet of the working fluid evaporator;
  • the inlet of the heating agent channel of the working fluid evaporator is connected to at least one of the following positions of the vacuum sublimation evaporation cold heat energy separation system:
  • the working medium evaporator is the condenser or cooler in the compressor unit in the vacuum sublimation evaporation unit.
  • the inlet of the coolant channel of the working fluid condenser is directly or indirectly connected to the ice slurry outlet of the container.
  • the vacuum sublimation evaporation unit is a compressor, which can be a multi-stage axial flow compressor, or even a multi-stage axial flow with counter-rotating structure Compressor, such a compressor has a large mass flow rate, through the design of the compressor structure and pressure ratio in the vacuum sublimation evaporation unit, the configuration of the condenser and cooler, the steam can be extracted with a large mass flow rate, therefore, it can be realized Efficiently extract the vapor generated from the liquid state through vacuum sublimation evaporation from the container, and maintain the vacuum condition in the container, and can quickly complete the separation of cold and heat energy.
  • a compressor which can be a multi-stage axial flow compressor, or even a multi-stage axial flow with counter-rotating structure Compressor, such a compressor has a large mass flow rate, through the design of the compressor structure and pressure ratio in the vacuum sublimation evaporation unit, the configuration of the condenser and cooler, the steam can be extracted with a large mass flow rate
  • the use of the cold and heat energy separation system has a positive impact on energy-saving applications such as seawater desalination.
  • the working medium for power generation is heated and vaporized by the steam extracted by the vacuum sublimation evaporation unit in the vacuum sublimation evaporation cold-heat energy separation system or the cooled or condensed hot water, so that the ice slurry discharged from the container in the cold-heat separation system is used
  • the coolant of the condenser the working medium is liquefied, which solves the problem that the seawater temperature difference power generation depends on the heat energy temperature difference of the seawater surface is too small and needs to transport a large amount of seawater.
  • Fig. 1 is a schematic structural diagram of a vacuum sublimation evaporation cooling and heat energy separation system provided by the present invention.
  • FIG. 2 is a schematic structural view of the vacuum sublimation evaporation unit in the separation system of Example 1.
  • FIG. 2 is a schematic structural view of the vacuum sublimation evaporation unit in the separation system of Example 1.
  • Fig. 3 is a structural schematic diagram of the vacuum sublimation evaporation unit in the separation system of Example 2.
  • Fig. 4 is a schematic structural diagram of the vacuum sublimation evaporation unit in the separation system of Example 3.
  • FIG. 5 is a schematic structural diagram of the vacuum sublimation evaporation unit in the separation system of Example 4.
  • FIG. 5 is a schematic structural diagram of the vacuum sublimation evaporation unit in the separation system of Example 4.
  • Fig. 6 is a structural schematic diagram of a multi-stage axial flow compressor.
  • Fig. 7 is a structural schematic diagram of a device for adding cooling to the motor in the compressor shown in Fig. 6 .
  • Fig. 8 is a structural schematic diagram of changing the cylindrical casing of the compressor shown in Fig. 7 to a compressor with a conical casing at one end.
  • Fig. 9 is a structural schematic diagram of a counter-rotating compressor.
  • Fig. 10 is a structural schematic diagram of another counter-rotating compressor.
  • Fig. 11 is a schematic diagram of an open cycle for generating electricity using seawater temperature difference.
  • Fig. 12 is a schematic diagram of a closed cycle for generating electricity using seawater temperature difference.
  • Fig. 13 is a schematic diagram of Scheme 1 for power generation by using the vacuum sublimation evaporation cold and heat energy separation system.
  • Fig. 14 is a schematic diagram of Scheme 2 for power generation using a vacuum sublimation evaporation cold and heat energy separation system.
  • Fig. 15 is a schematic diagram of Scheme 3 for power generation using a vacuum sublimation evaporation cold and heat energy separation system.
  • the high-efficiency vacuum sublimation evaporation cold and heat energy separation system includes a sealed container, which can also be called a crystallizer 1.
  • An artificial environment is formed in the crystallizer 1, and in the crystallizer 1
  • a liquid inlet 11 , a steam outlet 12 and a solid-liquid mixture outlet 13 are provided, and a vacuum sublimation evaporation unit 2 is connected to the steam outlet 12 , and an agitator 14 is also provided in the crystallizer 1 .
  • vacuum is evacuated by the vacuum sublimation evaporation unit 2 to form the vacuum environment of the aforementioned artificial environment.
  • Liquid such as water
  • the water evaporates and sublimes in a vacuum in the vacuum environment in the crystallizer 1, and the vaporized steam
  • the steam is continuously extracted from the steam outlet 12 by the vacuum sublimation evaporation unit 2, and the extracted steam is compressed by the compressor to increase the pressure and temperature of the steam. 13 is discharged, thereby completing the separation of cold and heat energy.
  • Table 2 lists the compressor power values under various pressure ratios.
  • P1 is the inlet pressure of the vacuum sublimation evaporation unit, that is, the pressure in the crystallizer 1
  • P2 is the outlet pressure of the vacuum sublimation evaporation unit
  • T1 is the temperature in the crystallizer 1
  • T2 is the outlet pressure of the vacuum sublimation evaporation unit.
  • Temperature P is the motor power of the vacuum sublimation evaporation unit.
  • the vacuum sublimation evaporation unit uses a compressor with a large flow rate.
  • the vacuum sublimation evaporation unit 2 adopts two multi-stage axial flow compressors connected in series to form an axial flow compressor unit, as shown in Fig. 2 .
  • the pressure ratio of the first multistage axial flow compressor 21 is 20 (the pressure can reach 10,000Pa from 500Pa)
  • the pressure ratio of the second multistage axial flow compressor 22 is more than 10 (the pressure can be from 10000Pa reaches the atmospheric pressure above 101320Pa), which can realize the direct separation of atmospheric pressure water vapor above 100 °C, and realize the separation of heat energy.
  • the low-temperature engine can produce about 500 kilowatts of electricity with an efficiency of 8-12%.
  • the COP of Scheme 1 can also reach about 3.6.
  • the remaining 80% heat 4000KWH after power generation can still be used continuously.
  • the problem in this embodiment is that it is difficult to manufacture a compressor with such a high pressure ratio, and the cost is also relatively high.
  • the vacuum sublimation evaporation unit 2 still adopts two multi-stage axial flow compressors, but the difference is that a condenser 23 is connected to the gas outlet of the first multi-stage axial flow compressor 21 , most of the water vapor extracted by the compressor 21 is condensed into water, and the separated thermal energy is obtained in the form of hot water. water vapor).
  • the gas outlet of the condenser 23 is connected to the second multi-stage axial flow compressor 22 .
  • the vacuum sublimation evaporation unit 2 includes a multistage axial flow compressor 21 , a condenser 23 and a screw vacuum pump system 24 .
  • the steam outlet 12 of the crystallizer 1 is connected to the inlet of the multi-stage axial flow compressor 21, the outlet of the compressor 21 is connected to the steam inlet of the condenser 23, the steam outlet of the condenser 23 is connected to the screw vacuum pump system 24, and the outlet of the vacuum pump 24 is emptied.
  • Table 3 lists the data of the outlet temperature of the compressor 21 and the corresponding equilibrium pressure P2.
  • the outlet pressure of the compressor 21-1 is 7500Pa
  • the pressure ratio is 15, and the corresponding gas-liquid equilibrium temperature is 40.5°C.
  • the temperature of the water vapor extracted from the crystallizer 1 by the axial flow compressor 21 is 40.5°C
  • the normal temperature water in the natural state is generally about 20°C, and the water vapor will release heat and condense into crystal water.
  • the temperature difference can reach about 20°C, which can fully meet the conditions of heat exchange and condensation of 70%-90% water vapor.
  • the screw vacuum pump 24 extracts a small amount of remaining water vapor in the condenser 23 for use or is emptied.
  • a vacuum pump may also be connected.
  • the vacuum sublimation evaporation unit 2 includes a multistage axial flow compressor 21 , a cooler 25 , a centrifugal compressor 26 , a condenser 23 and a screw vacuum pump 24 . Its sequence is connected in series.
  • the steam outlet 12 of the crystallizer 1 is connected to the inlet of the multi-stage axial flow compressor 21, the outlet of the compressor 21 is connected to the steam inlet of the cooler 26, and the steam outlet of the cooler 26 is connected to the inlet of the centrifugal compressor 26, and the centrifugal compressor
  • the outlet of the machine 26 is connected to the steam inlet of the condenser 23, the steam outlet of the condenser 23 is connected to the screw vacuum pump system 24, and the outlet of the vacuum pump 24 is emptied.
  • the cooler 25 only cools the incoming steam but does not allow it to precipitate condensed water, and the cooled steam enters the centrifugal compressor 26 for repressurization, which can reach 10000 Pa, and then the steam enters the condenser to Most of the steam condenses into water, and a small amount of water vapor is exhausted by the screw vacuum pump 24.
  • a cooler is installed between the two compressors to reduce the temperature of the steam and improve efficiency.
  • Table 4 is a comparison of the cost of heat energy obtained by various fuels (taking heating 1 ton of normal temperature water to 60 degrees as an example).
  • the above separation system schemes only calculate the thermal energy efficiency of separation.
  • the air compressor used in the present invention can be a multi-stage axial flow air compressor as shown in Figure 6, which is provided with a suction port 201 and an exhaust port 202, and the air suction port 201 and the gas outlet 12 of the crystallizer 1 or with The outlet of the previous compressor is connected, or is connected with the discharge outlet of the previous cooler or condenser, and the exhaust port 202 is connected with the inlet of the latter stage compressor or cooler or condenser.
  • the compressor used in the previous embodiments may have such a structure: the multistage axial flow compressor includes a casing 203, and the motor 204 of the compressor is arranged in the casing 203, the motor 204 is a two-axis motor in which an output shaft is provided at each of its two ends and the two output shafts are coaxial. A number of rotor blades are respectively fixed on the two output shafts, and stator blades are arranged between adjacent rotor blades. The blades are fixed on the casing 203 . The same number of moving blades are arranged symmetrically on the two output shafts. As shown in FIG.
  • three rotor blades A are arranged on the output shaft on the left side of the motor 204
  • three rotor blades B are arranged on the output shaft on the right side of the motor 204
  • the stator blades C are provided between the respective rotor blades.
  • an equal number of moving blades are symmetrically arranged on both sides of the motor 204, so that the power on both sides is balanced, and the motor is arranged in the middle, and the stator blades are arranged in the casing where the motor is located, so that Make the structure of the compressor more compact.
  • the ends of the hub are recessed, and a part of the two ends of the motor body is accommodated in the recessed space, that is, the part of the hub where the blades are connected to the motor shaft is on the output shaft, but
  • the blades are extended to the outside of the casing of the motor, and such a design can also make the structure of the compressor compact.
  • a gap is provided between the motor casing and adjacent rotor blades.
  • stator vane In the middle of the casing of the motor 204, a stator vane is arranged, and the stator vane can also play the role of supporting the motor. It is more stable fixed in the chassis.
  • four rotor blades are respectively symmetrically fixed on the output shafts on both sides of the motor.
  • an accommodating cavity can be provided inside the stator blade C1 in the middle of the motor casing, and a coil C2 is arranged in it, and the two ends of the coil C2 are separated from the casing of the compressor along the stator blade. Stretch out (not shown in the figure), communicate with coolant, the motor is cooled and lowered in temperature.
  • the casing of the multi-stage axial flow compressor is composed of a section of conical barrel 203-1 and a section of cylindrical barrel 203-2.
  • the large-diameter end of the cylinder is the inlet end 201 of the air compressor.
  • the multi-stage axial flow compressor can adopt a counter-rotating structure.
  • two multi-stage axial flow compressors as shown in Figure 6 and Figure 7 are connected end to end, however, the rotation direction of the impeller in the latter compressor is opposite to that of the previous compressor, and the operation During the process, the direction of rotation of the motor is reversed.
  • the multi-stage series connection can reach a pressure ratio of 16-20.
  • the separation method using the separation system includes the step of using the vacuum sublimation evaporation unit to extract steam from the container, in this step, the steam extracted from the previous compressor enters the A heat exchanger, the condenser, is introduced before the next compressor, in which 70-90% of the steam is condensed.
  • a heat exchanger is added, and in the process of extracting steam, the pressure ratio of each compressor in the vacuum sublimation evaporation unit is 2-20; for example, the pressure ratio can be reduced to 2, using several stages of compressors or several compressors in series , can make the pressure ratio of each stage or each compressor lower, while the energy consumption of the entire vacuum sublimation evaporation unit is reduced, and the COP value is greatly increased.
  • the coolant in the heat exchanger is normal temperature air or water.
  • Reasonable arrangement of the number of stages or sets of compressors can also make the temperature of the extracted steam higher than the temperature of water or air at room temperature, and this temperature difference can be cooled with water or air at room temperature, making this process very convenient and low-cost proceed.
  • the coolant in the heat exchanger is the condensed water extracted from the subsequent heat exchanger.
  • the condensed water of the rear heat exchanger can also be directly used as the coolant of the front heat exchanger. This can also increase the temperature of the coolant, so that the condensed water can be reused, such as low-temperature power generation.
  • the high-efficiency vacuum sublimation evaporation cold-heat energy separation system provided by the invention can also be used for power generation.
  • the power generation system includes a steam turbine 31 and a generator 32.
  • the steam turbine 31 is provided with a fresh steam inlet and a exhaust steam outlet.
  • the shaft of the steam turbine 32 is connected to the power generator.
  • the rotor of the machine in the prior art, is provided with a flash evaporator 033, the warm sea water will be introduced into the flash evaporator 033 in a vacuum state through the warm sea water pump 036, to make it partially evaporate, and its vapor pressure is about 3kPa (25 °C), which is equivalent to 0.03 Atmospheric pressure.
  • the water vapor undergoes adiabatic expansion in the low-pressure steam turbine 31 and is discharged after doing work.
  • the cold sea water pump 037 pumps cold sea water to condense the water vapor into a liquid.
  • the latter is the method for incidentally preparing fresh water (see Figure 11).
  • the flash evaporator 033 is replaced by the vacuum sublimation evaporation unit, and the steam extracted from the container 1 and compressed by the compressor is passed into the screw expander or steam turbine.
  • Method 1 uses the thermoelectric power generation system of the open cycle system, in combination with the above-mentioned embodiment 1, uses two multi-stage axial flow compressors 21 and 22 to form the vacuum sublimation evaporation unit 2 to extract from the container 1
  • the extracted steam is compressed and directly passes through the screw expander or steam turbine to generate electricity. Since the steam outlet pressure is 7500Pa and the temperature is above 200°, it is much better than the original operation scheme and should have higher power generation efficiency.
  • An open circulation system does not use a working medium (working fluid).
  • the closed circulation system uses a working fluid with a low boiling point as a working medium.
  • Its main components include an evaporator 33, a condenser 34, a turbine 31, and a generator 32, and also include a working medium pump 035, a warm sea water pump 036, and a cold sea water pump 037.
  • the warm sea water is pumped up by the warm sea water pump, the heat source is transferred to the working medium in the evaporator to evaporate it.
  • the evaporated working fluid expands adiabatically in the turbine and pushes the blades of the turbine to generate electricity.
  • the working fluid after power generation is introduced into the condenser, and its heat is transferred to the cold seawater pumped from the deep layer, so it is cooled and restored to liquid, and then pumped to the evaporator by a circulating pump to form a cycle.
  • the working medium can be used repeatedly, and its types include ammonia, butane, chlorofluorocarbons and other gas refrigerants with high density and high vapor pressure. Ammonia and chlorofluorocarbons are the most likely working fluids.
  • the energy conversion efficiency of the closed cycle system is between 3.3% and 3.5%. If the energy consumption of the pump is deducted, the net efficiency is between 2.1% and 2.3%.
  • the evaporator 33 of the heating working medium is improved, and the steam or condensed water in the vacuum sublimation evaporation unit 2 is introduced into the evaporator 33 to replace the warm seawater, or the condenser 23 in the vacuum sublimation evaporation unit 2 is replaced by the working fluid. mass evaporator.
  • Method 2 As shown in Figure 14, directly introduce the 50°-70° hot water discharged from the condenser 23 of the vacuum sublimation evaporation unit power in the vacuum sublimation evaporation cooling and heat energy separation system in the above embodiment 4 into seawater temperature difference power generation system, the hot water passes into the evaporator 33 in the closed cycle system, and the heating medium makes it obtain energy to do work.
  • the power generation efficiency should be 8%-10%.
  • Method 3 combines the evaporator 33 in the closed cycle system of seawater thermoelectric power generation with the condenser 23 of the vacuum sublimation evaporation unit power in the vacuum sublimation evaporation cooling and heat energy separation system in the above-mentioned embodiment 4.
  • This working parameter is much better than the conditions of 3300Pa pressure and 25° steam outlet temperature of the seawater temperature difference power generation system. The temperature difference is greatly increased, and the power generation efficiency should be around 15%, which can meet the needs of commercialization.
  • the working fluid is still circulated through the working fluid pump 035 .
  • the condensation of the working fluid can use the ice slurry discharged from the container 1 . That is, the coolant channel in the condenser 34 directly or indirectly introduces the ice slurry discharged from the container 1 .
  • first and second are used for descriptive purposes only, and should not be understood as indicating or implying relative importance or implicitly specifying the quantity of indicated technical features. Thus, a feature defined as “first” and “second” may explicitly or implicitly include one or more of these features. In the description of the present invention, “plurality” means two or more, unless otherwise specifically defined.
  • the terms “mounted”, “connected”, “connected”, “fixed” and other terms should be interpreted in a broad sense, for example, it may be fixedly connected or detachably connected, or integrated; it may be mechanically connected or It can be an electrical connection, or it can be a communication; it can be a direct connection or an indirect connection through an intermediary, it can be the internal communication of two components or the interaction between two components, and the "connection” can also be connected through a pipeline.

Abstract

本发明提供一种高效率的真空升华蒸发冷热能分离系统，其中的分离系统包括一个密封的容器，在该容器上设有液体进口、气体出口和固体或固液混合物出口；在该气体出口上连接一真空升华蒸发机组，为密封容器提供设定的蒸发压力；所述真空升华蒸发机组为一压气机组，其包括至少一台压气机，该压气机上设有吸气口和排气口，所述吸气口与所述容器的气体出口连接。本发明还提供分离方法，其中给出真空升华蒸发机组的压气机的各种压比设计，本发明通过分离系统和相应的分离方法可以大流量抽吸容器中真空蒸发所产生的水蒸汽以提高冷热能的分离效率。

Description

高效率的真空升华蒸发冷热能分离系统和分离方法及其应用 技术领域
本发明属于绿色能源技术领域，涉及一种真空升华蒸发冷热能分离系统，尤其提供一种高效率的真空升华蒸发冷热能分离系统，还提供使用该分离系统的分离方法。另外，还提供该分离系统在海洋温差发电中的应用。
背景技术
真空升华蒸发冷热能分离技术是一种利用真空蒸发和升华分离水中能量的技术。水中含有大量的能量，用一吨0℃水结成冰所释放出来的结晶潜热可将一吨20℃的常温水加热到100℃，能量可达93KWH。而对比筑水坝发电，一吨水在超百米高度落差条件下，势能仅能发电0.3KWH左右，仅为一吨水中结晶潜热能量的0.32％，即等量水中的结晶潜热是水百米落差势能的290倍左右。以长江为例，三峡大坝每年发电1000亿度左右，长江流量近10000亿吨/年。(我国全年发电量72255亿度，民用电10248亿度。计算可知三峡发电量为全国总发电量的1.38％)。而该流域水量所含结晶潜热930000亿度左右。发电量仅为所含结晶潜热的千分之一左右。
水也是很好的储能载体，很好实现了对地球温度的调节。与现有储能电池作比较，见下表1：
表1
Figure PCTCN2022116936-appb-000001
从表1可见，仅从储能的角度看，1吨常温水储存的热能(显热和结晶潜热)是铅电池的近三倍，是最热门的锂电池的1/2，可见储能能力巨大。
分离出的能量可使热能以热水或蒸汽的形式保存，冷能以冰浆或冰块的形式保存，并加以利用。35-40度的热水即可用于冬季采暖，农用温室大棚的种植、养殖等生产活动。即使在我国北方冬季，河流冰层下的流水，依然保存着巨大的能量。分离出热能后的冰可在适当的季节或条件下自然融化。可为无霜期短的广大地区提供新的生产模式。分离出的冷能则可以用于制冰、夏季的空调(地冷，16-18度冷水即可实现)以及为农产品保鲜提供冷源等生 产活动。运用冷冻法也可用于海水、苦咸水淡化，开辟新的水源。该冷热能分离技术是一种用途非常广泛且非常具有发展前景的绿色能源技术。
海洋温差发电的提出，是基于海水表面和深部有大约20℃温差的现象提出的，其原理如图11和图12所示，但百年已过，却一直没有商业化，且原因之一就在于只是利用海水中的显热做功发电，使得吨水使用热能不足，造成发电效率低，需要海水量大，深部海水的抽取还要消耗大量的能源。冷热能分离是将液体的潜热利用起来，这样势必比起只利用液体显热可以大大提高发电效率、减小水的输送量，现有技术中没有这样的方案。
如图1所示，在该冷热能分离系统中包括一个密封的容器1，还包括一抽真空系统2，对容器1抽真空，以形成一个使得水能够在其中真空蒸发的人造环境。要使得容器1中能够保持一个设定的真空工况，使其中的水能够不断地蒸发，以获得高效率的分离冷热能的效果，将水蒸气从人造真空环境中高效抽出是最为关键的步骤。在500Pa的真空环境下，水蒸气的密度大大降低，是大气压力条件下的二百分之一左右。在此条件下完全使用现有的真空泵系统，质量流量将会很小，由此使得分离效率不高。
为了提高冷热能分离的效率，就需要配置一个大质量流量的抽真空系统。如何才能使得抽真空系统具有大质量流量，从而使得冷热能分离高效率地进行，是本发明要解决的技术问题。
发明内容
本发明的目的在于提供一种高效率的真空升华蒸发冷热能分离系统，其中的抽真空系统可以大流量抽吸容器中真空蒸发所产生的水蒸汽以提高冷热能的分离效率。
本发明的另一个目的是提供使用该分离系统的分离方法。
本发明的再一个目的是提供一种利用前述高效率的真空升华蒸发冷热能分离系统进行发电的系统和方法。
本发明的目的是这样实现的：
一种高效率的真空升华蒸发冷热能分离系统，包括一个密封的容器，在该容器上设有液体进口、气体出口和固体或固液混合物出口；在该气体出口上连接一抽真空系统，其为一真空升华蒸发机组，连续高效地抽出所述容器中的蒸汽，为密封容器提供设定的蒸发压力；
所述真空升华蒸发机组为一压气机组，其包括至少一台压气机，该压气机上设有吸气口和排气口，该压气机的吸气口与所述容器的气体出口连接。
进一步地，所述压气机组包括至少两台压气机，各台压气机串联连接。
优选地，所述压气机可以是轴流式压气机，也可以是离心式压缩机。
优选地，所述轴流式压气机为多级轴流式压气机。
具体地，一个关于多级轴流式压气机的优选方案是：所述多级轴流式压气机包括一个机壳，在该机壳中设置该压气机的电机，该电机为其两端各设置一输出轴且两根输出轴同轴线的双轴电机，在两根输出轴上分别固设有若干转子叶片，在相邻的转子叶片之间设置静子叶片，该静子叶片固定在所述机壳上。
优选地，在两根输出轴上对称地设置数量相同的转子叶片。
优选地，在每根所述输出轴上设置2-4个所述转子叶片。
优选地，在所述电机两侧与所述电机相邻的转子叶片的轮毂的端部内凹，电机机身两端的至少一部分容纳在内凹的空间中，在两个与电机相邻的转子叶片之间的电机机身上设置静叶片。
优选地，在所述电机机身上设置所述静子叶片处设有冷却装置，以利于电机散热。
该静子叶片成为所述电机在所述机壳中的支架。在该支架上设置电源输入端口和冷却装置的输入输出端口。
优选地，所述多级轴流式压气机机壳由一段圆锥形筒和一段圆柱形筒组成，该圆锥形筒的大直径一端为该压气机的进口端。
进一步地，所述多级轴流式压气机为对旋式压气机，即包括两个多级轴流压气机，两个压气机的机壳密封连接，两个多级轴流压气机中的叶轮的旋向相反，电机转向相反，形成对旋效应。
优选地，所述真空升华蒸发机组中还包括换热器，作为冷却器和/或冷凝器，其中设置蒸汽通道和冷却剂通道，该蒸汽通道的进口与在前的所述压气机的排气口连接，以对所述压气机抽出的蒸汽冷却或冷凝。
优选地，所述真空升华蒸发机组中还包括一真空泵，该真空泵的出口与大气连通，其入口连接在前的所述压气机换热器。
下面是几个所述真空升华蒸发机组的优选方案：
方案1：包括一台多级轴流式压气机和一台真空泵，其串联连接，所述多级轴流式压气机的进气口连接所述容器的气体出口，所述真空泵的出气口与大气连通。
方案2：包括一台对旋结构的多级轴流式压气机、一台冷凝器和一台真空泵，其顺序串联连接，所述多级轴流式压气机的进气口连接所述容器的气体出口，所述真空泵的出气口与大气连通。
方案3：包括一台对旋结构的多级轴流式压气机和一台离心式压缩机，其串联连接。
方案4：包括一台对旋结构的多级轴流式压气机、一台冷却器、一台压气机、一台冷凝器和一台真空泵，其顺序串联连接，其中的压气机为对旋结构的多级轴流式压气机或离心式压缩机。
优选地，所述真空升华蒸发机组为两台以上轴流压气机，还包括一组气-液换热器，即冷凝器，所述气-液换热器上设有进气口、出气口和排液口，所述进气口连接第一台所述压气机的所述排气口，所述出气口连接第二台所述压气机的进气口，第二台所述压气机上的排气口与大气连通；所述排液口连接管路系统以收集热水加以利用。
为了提高分离效率，就必须引入大流量的高效真空系统。轴流压气机或离心压缩机作为真空环境出口处的水蒸气抽出设备，抽出的水蒸气经压缩升压并随后通入串联的换热器。这样的换热器的功能要求也从简单冷却降温变为可实现对抽出的水蒸气实现70％-90％左右的冷凝，直接产生一定温度的冷凝水。以获得较好的热能分离效果。
为提高系统运行的可靠性并降低成本，优选该改进型初级压气机和离心压缩机组成压气机组。
优选地，所述真空升华蒸发机组还包括一组气-液换热器即冷凝器和一真空泵，所述冷凝器包括一个壳体，在该壳上设有进气口、出气口和排液口，所述进气口连接所述压气机的所述排气口，所述出气口连接所述真空泵的进气口，所述真空泵上的排气口与大气连通。
通过多台压气机组与多台气-液换热器的多种形式组合，以实现高效分离水中潜热和显热达到规模使用的目的。
优选地，所述真空泵为螺杆式真空泵。
本发明提供的使用上述分离系统的真空升华蒸发冷热能分离方法，其中包括使用所述真空升华蒸发机组从所述容器中抽取蒸汽的步骤。
进一步地，在该步骤中，在前一个压气机抽出的蒸汽在进入下一个压气机之前先引入一换热器，作为冷却器或冷凝器，在该冷却器中，将由前面的压气机抽出的蒸汽降温，在该冷凝器中，将其中70-90％的蒸汽冷凝下来。
在抽取蒸汽步骤中，所述真空升华蒸发机组中各个压气机的压比范围在2-20。
如下是几个抽取蒸汽步骤中的优选方案：
方案1：抽取蒸汽步骤中，通过二级压气机直接抽出水蒸气：第一级压气机压比：15，串联第二级压气机压比：15，总压比：225。
方案2：不直接抽出水蒸气，而是通过换热器将水蒸汽冷凝。
抽取蒸汽步骤中，第一级压气机压比：15-16，对应气液平衡压力7500Pa-8000Pa，温度40.5℃，随后，蒸汽进入串联的换热器，将70％-90％的水蒸汽冷凝为温水，之后，进入第二级压气机，其压比：15，抽出剩余的水蒸气。
方案3：不直接抽出水蒸气，而是通过换热器将水蒸汽冷凝。
抽取蒸汽步骤中，第一级压气机压比：15-16，对应气液平衡压力7500Pa-8000Pa，温度40.5℃，随后，蒸汽进入串联换热器，将70％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出口被后面串联的螺杆真空泵抽出。
方案4：不直接抽出水蒸气，而是通过换热器将水蒸汽冷凝。
抽取蒸汽步骤中，第一级压气机压比：4，随后串联换热器降温，再串联一台离心压缩机，其压比：4，总压比为16，对应气液平衡压力7500Pa-8000Pa，温度40.5℃，随后，蒸汽进入串联换热器将70％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出口被后面串联的螺杆真空泵抽出。
方案5：不直接抽出水蒸气，而是通过换热器将水蒸汽冷凝。
第一级压气机压比：3-4，对应气液平衡压力1500Pa-2000Pa，温度13°-17℃，随后蒸汽进入串联冷凝器，输入的冷却介质温度2℃以下，将40％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出口被后面串联的压气机和/或螺杆真空泵抽出。
该方法适用于海水淡化生产为主的应用。
在抽取蒸汽步骤中，所述冷却器和/或冷凝器中的冷却剂为常温空气或水，例如20-30℃的空气或水。
在抽取蒸汽过程中，所述冷却器和/或冷凝器中的冷却剂可以为在后的所述冷凝器中排出的冷凝水。
利用不同的工艺条件设计，在未达到大气压前，利用冷凝器将压气机抽出的水蒸气70％-90％冷凝成结晶水(50度以上)，作为热能量输出。由于不同压比的压气机组输出的蒸汽压力不同，冷凝温度也不同，本发明提供了完善工艺设计，获得高效能量分离的多种可能。
利用前述高效率的真空升华蒸发冷热能分离系统进行发电方法，其中包括一发电系统，该发电系统包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，其特征是：将所述真空升华蒸发机组中的蒸汽通入所述螺杆膨胀机或汽轮机。
进一步地，所述发电系统包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一工质新蒸汽进口和一工质乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所 述发电机的转子，还包括一工质蒸发器和一工质泠凝器，所述工质蒸发器中设有相变工质流道和加热剂流道，工质蒸发器中的相变工质流道的两端分别是液态工质进口和气态工质蒸汽出口，所述工质冷凝器中设有相变工质流道和冷却剂流道，工质冷凝器中的相变工质流道的两端分别是工质乏蒸汽进口和液态工质出口，所述工质蒸发器的气态工质蒸汽出口连接所述螺杆膨胀机或汽轮机的工质新蒸汽进口，所述螺杆膨胀机或汽轮机的乏蒸汽出口连接所述工质冷凝器的工质乏蒸汽进口，所述工质冷凝器的液态工质出口连接所述工质蒸发器的液态工质进口；其特征是：
在所述工质蒸发器的加热剂流道中通入所述真空升华蒸发机组中的蒸汽或热水，用以将工质加热成蒸汽通入所述螺杆膨胀机或汽轮机。
具体地，
可以是将所述工质蒸发器中所述加热剂流道的进口连接到所述真空升华蒸发机组中所述压气机组上的排气口；
或者连接所述真空升华蒸发机组中所述压气机组后面连接的所述冷凝器或冷却器的出口；
或者将所述工质蒸发器和所述真空升华蒸发机组中的冷凝器或冷却器合二为一，压气机排出的蒸汽或热水对工质进行加热，然后再排放。
所述工质冷凝器中所述冷却剂流道直接或间接地引入所述容器中排出的冰浆。
上述发电系统为：
包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，所述真空升华蒸发机组中的所述压气机组的蒸汽出口连接所述螺杆膨胀机或汽轮机的所述新蒸汽进口。或者，
包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，还包括一工质蒸发器和一工质冷凝器，所述工质蒸发器中设有相变工质流道和加热剂流道，工质蒸发器中的相变工质流道的两端分别是液态工质进口和新气态工质蒸汽出口，所述工质冷凝器中设有相变工质流道和冷却剂流道，工质冷凝器中的相变工质流道的两端分别是工质乏蒸汽进口和新液态工质出口，所述工质蒸发器的新气态工质蒸汽出口连接所述汽轮机的蒸汽进口，所述汽轮机的乏蒸汽出口连接所述工质冷凝器的工质乏蒸汽进口，所述工质冷凝器的新液态工质出口连接所述工质蒸发器的液态工质进口；
所述工质蒸发器的加热剂流道的进口连接所述真空升华蒸发冷热能分离系统的如下位置 至少其中之一：
所述真空升华蒸发机组中所述压气机组上的排气口；
所述真空升华蒸发机组中所述压气机组中的所述冷凝器或冷却器的出口；
所述真空升华蒸发机组中所述压气机的出口；
所述工质蒸发器即为所述真空升华蒸发机组中所述压气机组中的所述冷凝器或冷却器。
所述工质冷凝器的冷却剂流道的进口直接或间接连接所述容器的冰浆出口。
本发明提供的高效率的真空升华蒸发冷热能分离系统和分离方法，其中的真空升华蒸发机组为压气机，其可以是多级轴流式压气机，甚至是对旋结构的多级轴流压气机，这样的压气机由于其质量流量较大，通过对于真空升华蒸发机组中压气机结构和压比的设计，冷凝器、冷却器的设置，可以大的质量流量抽出蒸汽，因此，可以实现高效率地从容器中抽出从液态通过真空升华蒸发而产生的蒸汽，维持容器内的真空条件的目的，可以快速地完成冷热能的分离。使得利用冷热能分离系统在诸如海水淡化等方面的节能应用上起到积极影响。而将发电的工质利用真空升华蒸发冷热能分离系统中的真空升华蒸发机组抽出的蒸汽或经冷却或冷凝后的热水进行加热汽化，以至于用冷热分离系统中容器排出的冰浆作为冷凝器的冷却剂将工质液化，很好地解决了海水温差发电单靠海水表面的热能温差太小和需要输送大量海水的问题。下面结合附图和实施例对本发明做详细说明。
附图说明
图1为本发明提供的真空升华蒸发冷热能分离系统的结构示意图。
图2为实施例1的分离系统中真空升华蒸发机组的结构示意图。
图3为实施例2的分离系统中真空升华蒸发机组的结构示意图。
图4为实施例3的分离系统中真空升华蒸发机组的结构示意图。
图5为实施例4的分离系统中真空升华蒸发机组的结构示意图。
图6为一种多级轴流式压气机的结构示意图。
图7为在图6所示压气机中增加对于电机冷却的装置的结构示意图。
图8为在图7所示压气机中改圆筒形机壳改为包含一端圆锥筒机壳压气机的结构示意图。
图9为一种对旋结构压气机的结构示意图。
图10为另一种对旋结构压气机的结构示意图。
图11为利用海水温差发电的开式循环示意图。
图12为利用海水温差发电的闭式循环示意图。
图13为利用真空升华蒸发冷热能分离系统进行发电的方案1的示意图。
图14为利用真空升华蒸发冷热能分离系统进行发电的方案2的示意图。
图15为利用真空升华蒸发冷热能分离系统进行发电的方案3的示意图。
具体实施方式
如图1所示，本发明提供的高效率的真空升华蒸发冷热能分离系统，包括一个密封的容器，也可以称为是结晶器1，结晶器1内构成一人造环境，结晶器1中设有液体进口11、蒸汽出口12和固液混合物出口13，在该蒸汽出口12上连接一真空升华蒸发机组2，在结晶器1中还设有搅拌器14。
在结晶器1中通过真空升华蒸发机组2抽真空，构成前述人造环境的真空环境，液体，例如水由液体进口11输入，水在结晶器1内的真空环境中真空蒸发升华，气化的蒸汽不断地由蒸汽出口12被真空升华蒸发机组2抽出，抽出的蒸汽经压气机压缩使蒸汽压力温度升高，留在结晶器1内的水由于失去热量即结冰，冰浆固液混合物从出口13排出，由此完成冷热能分离。
实现将水的能量进行分离，需要在绝对压力500Pa以下的环境中进行能量分离。在出口为大气压力条件下(绝对压力为101320Pa)，压比可达203。如使用轴流压气机真空系统，将500帕环境中的水蒸气抽出并排入大气，压缩比需200以上。以此条件并根据如下公式可计算出轴流压机真空系统的功率，计算公式及结果列表如下：
1.不同压比压气机的电机功率估算公式：
P＝qm*Cp*T1*(π^((k-1)/k)-1)/eta/1000，
其中：
P：电机功率，qm：质量流量，Cp：定压比热，Cp＝k/(k-1)*R＝2002J/kgk，
eta：绝热效率：eta＝0.8，π：压比，COP：能耗比，T1：入口温度，K：比热比，K＝1.3，气体常数：R(J/KgK)＝462。
2.不同压比下出口温度计算公式：
温差＝T1*(π^((k-1)/k)-1)/eta
表2中列出了各种压比下压缩机功率值。
表2
Figure PCTCN2022116936-appb-000002
Figure PCTCN2022116936-appb-000003
表2中，P1为真空升华蒸发机组的入口压力，即结晶器1中的压力，P2为真空升华蒸发机组的出口压力，T1为结晶器1中的温度，T2为真空升华蒸发机组排出口的温度，P为真空升华蒸发机组的电机功率。
从上表可看出，随压比的上升，所需功率消耗也随之大幅增加，蒸汽的出口温度也大幅上升。
在本发明中，真空升华蒸发机组使用大流量的压气机。
为实现节能高效的目的，由此产生多个方案，以下为主要的几个方案。如下实施例只是作为举例，本发明的保护范围以权利要求书为准。
实施例1：
真空升华蒸发机组2采用两台多级轴流式压气机串联构成轴流压气机组，如图2所示。当采用第一台多级轴流式压气机21的压比为20(压力可从500Pa达到10,000Pa)，第二台多级轴流式压气机22的压比为10以上时(压力可从10000Pa达到大气压101320Pa以上)，可实现直接分离出100℃以上常压水蒸气，实现热能分离。从表1中可得到两台压气机所消耗的功率为：1122KW+790KW＝1912KW。出口蒸汽温度400℃以上，分离出的水蒸气热能量大于：1335+3762＝5097，COP＞2.67。
从表1中可看到，随压比的增加，耗能增加，COP值减小。直接将水蒸气从500Pa条件下抽出达到大气压力，COP仅为2.67左右。
如将实施例1分离出的水蒸气用于发电，按低温发动机8～12％的效率，可产生500千瓦左右的电力。方案1的COP也可达到3.6左右。发电后剩余的80％热量4000KWH仍可继续使用。该实施例存在的问题是如此高的压比的压气机制造有一定难度，造价也较高。
实施例2：
为保证有良好效率，需采取相应措施，以提高能耗比。具体措施为，如图3所示，真空升华蒸发机组2还是采用两台多级轴流式压气机，但区别在于：在第一台多级轴流式压气机21出气口处连接冷凝器23，将压气机21抽出的大部分水蒸气凝结为水，以热水的形式获得分离的热能量，水温确定为50-70℃(后续还可间接以较小的能量消耗将该热水转换为水蒸气)。冷凝器23的出气口连接第二台多级轴流式压气机22。这样的真空升华蒸发机组，如第一台压气机21的压比在15-16，抽出的水蒸气在冷凝器23中有70％到90％被凝结为水，第二台多级轴流式压气机的功率将减少为原有功率的1/7以下，功率的初步计算结果为：1122KW+790/7＝1235KW，分离出的水蒸气热能量大于：788+3762＝4550。COP＝3.68，由此可以看出，在两级压气机之间增冷凝器23，可以使得效率大大提高。
实施例3：
如图4所示，真空升华蒸发机组2包括一台多级轴流式压气机21，一台冷凝器23和一台螺杆真空泵系统24。结晶器1的蒸汽出口12连接多级轴流式压气机21的进口，压气机21的出口连接冷凝器23的蒸汽进口，冷凝器23的蒸汽出口连接螺杆真空泵系统24，真空泵24的出口放空。
下面的表3列出压气机21的出口温度和对应的平衡压力P2的数据。
表3
P2(Pa) 气-液平衡温度℃ K
661 0 273
800 4 277
1000 7 280
1500 13 286
2000 17 290
2500 21 294
3000 24 297
3500 27 300
4000 29 302
5000 33 306
7500 40.5 313.5
10000 46 319
20000 60 333
30000 69 342
当压气机21-1出口压力为7500Pa时，压比＝15，对应气-液平衡温度为40.5℃，在此压力下，轴流压气机21从结晶器1中抽出的水蒸气温度是40.5℃以上，进入冷凝器23中， 与自然状态中常温水换热，自然状态中常温水一般为20℃左右，水蒸气便放出热量，凝结为结晶水。温差可达20℃左右，完全可以满足热交换冷凝70％-90％水蒸气的条件。螺杆真空泵24将冷凝器23中的少量剩余的水蒸气抽出利用或放空。
从表2中可看到，当末端压力为7500Pa，压比为15，功率为978KW，螺杆真空泵功率75KW，合计所需功率1053KW。分离热能量800+3762＝4562KWH，分离热能计算COP＝4.33。
实施例2中在第二台多级轴流式压气机22之后，也可以连接一台真空泵。
实施例4：
如图5所示，真空升华蒸发机组2包括一台多级轴流式压气机21，一台冷却器25、一台离心式压气机26、一台冷凝器23和一台螺杆真空泵24。其顺序串联连接。结晶器1的蒸汽出口12连接多级轴流式压气机21的进口，压气机21的出口连接冷却器26的蒸汽进口，冷却器26的蒸汽出口连接离心式压缩机26的进口，离心式压气机26的出口连接冷凝器23的蒸汽进口，冷凝器23的蒸汽出口连接螺杆真空泵系统24，真空泵24的出口放空。
在这个实施例中，冷却器25只是将进入的蒸汽进行冷却但不令其析出冷凝水，冷却后的蒸汽再进入离心式压气机26再次加压，可以达到10000Pa，然后该蒸汽进入冷凝器将大部分蒸汽冷凝成水，少量的水蒸气由螺杆式真空泵24排出放空。
在两台压气机之间设置一冷却器，降低蒸汽的温度，也可以提高效率。
根据以上的压气机在不同压比条件下的电机功率配置表，以及在不同压力下水的气液平衡温度表，可根据具体设备情况，设计多种工艺路径，以保证设备投入最少，能耗比最高，以取得最好的经济效益。
表4是各种燃料获取热能成本对比(以加热1吨常温水至60度为例)。
表4
Figure PCTCN2022116936-appb-000004
经计算真空蒸发技术获取热能的成本，在COP＝5，电价0.56元/度的条件下为112.7元 /MWH，与烧煤108元/MWH基本相同。如利用峰谷电价和新能源技术，电价可降至0.45元左右，90元/MWH的热能成本将明显低于烧煤成本，是空气能热水器的一半。而二氧化碳排放量也为空气能热水器的近一半。
以上各个分离系统方案，计算的仅为分离的热能效率，同时，结晶器1中还生成冰，排出冰浆，还应包含制冰的冷能(40吨冰)，如融化为0度水，释放冷能40*93KW＝3720KWH。冷热能合计：4322KWH+3720KWH＝8042KWH，综合能耗比COP＝11.7左右。
本发明使用的压气机可以是如图6所示的多级轴流式压气机，其上设有吸气口201和排气口202，吸气口201与结晶器1的气体出口12或者和前面的压气机的出口连接，或者和前面的冷却器或冷凝器的排出口连接，排气口202连接后一级的压气机或冷却器或冷凝器的进口。如图6所示，在前面的各个实施例中所使用的压气机可以是这样的结构：多级轴流压气机包括一个机壳203，在机壳203中设置该压气机的电机204，电机204为其两端各设置一输出轴且两根输出轴同轴线的双轴电机，在两根输出轴上分别固设有若干转子叶片，在相邻的转子叶片之间设置静子叶片，静子叶片固定在机壳203上。在两根输出轴上对称地设置数量相同的动叶片。如图6所示，在电机204的左侧的输出轴上设置三个转子叶片A，在电机204右侧的输出轴上设置三个转子叶片B。在各转子叶片之间设置静子叶片C。在多级轴流式压气机中，在电机204的两侧对称地设置数量相等的动叶片，使得两边动力平衡，而且电机设置在中间，在电机所在位置的机壳中设置静叶片，这样可以使得压气机的结构更加紧凑。另外，电机轴和靠近电机204的两个转子叶片，轮毂的端部内凹，电机机身两端的一部分容纳在该内凹的空间中，即叶片与电机轴连接的轮毂部分在输出轴上，但叶片延设到电机的壳体外面，这样的设计也能够使得压气机结构紧凑。电机机壳和相邻的转子叶片之间设有间隙。
在电机204的外壳的中间，设置一静子叶片，该静子叶片还可以起到支撑电机的支架作用，该静子叶片可以做的轴向长度比其他静子叶片更长一些，这样可以使得电机在压气机的机壳中固定的更加稳定。
一个更好的实例中，电机两侧的输出轴上分别对称地固设四个转子叶片。
另外，如图7所示，在电机外壳的中间的静子叶片C1的内侧可设置一个容置腔，在其中设有一盘管C2，该盘管C2的两端沿静子叶片从压气机的壳体伸出(图中未示出)，连通冷却剂，对电机进行冷却降温。
为了使得多级轴流式压气机的压气效果更好，如图8所示，多级轴流式压气机机壳由一段圆锥形筒203-1和一段圆柱形筒203-2组成，该圆锥形筒的大直径一端为该压气机的进口端201。
为了获得更高的压比，多级轴流式压气机可以是采用对旋结构。如图9所示，将两个如图6和如图7所示的多级轴流式压气机头尾相接，但是，后一个压气机中叶轮的旋向与前一个压气机相反，运行过程中，电机的转向相反。这样的对旋结构的多级轴流式压气机，多级串联可以达到压比16-20。
如图10所示，也可以将进口段为扩口的锥筒的压气机两个头尾相接，构成对旋结构的多级轴流式压气机。在上述各个实施例中，使用所述分离系统的分离方法，其中包括使用所述真空升华蒸发机组从所述容器中抽取蒸汽的步骤，在该步骤中，在前一个压气机抽出的蒸汽在进入下一个压气机之前先引入一换热器即冷凝器，在该换热器中将70-90％的蒸汽冷凝下来。
增加了换热器，在抽取蒸汽过程中，所述真空升华蒸发机组中各个压气机的压比在2-20；例如压比可以降低到2，使用几级压气机或几个串联的压气机，可以使得每级或每台压气机的压比较低，而整个真空升华蒸发机组的能耗却得到降低，大大提高COP值。
在抽取蒸汽过程中，所述换热器中的冷却剂为常温空气或水。合理地安排压气机的级数或台数，还可以使得抽出的蒸汽的温度高于室温下水或空气的温度，而这个温差能够用室温下的水或空气冷却，使得本过程可以很方便且低成本地进行。
在抽取蒸汽过程中，所述换热器中的冷却剂为后面的换热器抽出的冷凝水。通过合理设计各级压气机的压比，还可以直接采用后面换热器的冷凝水做前面换热器的冷却剂。这样还可以提高冷却剂的温度，从而可以使得这些冷凝水具有再利用，例如低温发电等使用。
也可以在两台压气机之间设置冷却器，即在冷却器中，不需要将蒸汽冷凝，只是对其降温，这样，也可以提高抽真空的效率。
本发明提供的高效率的真空升华蒸发冷热能分离系统也可以用于发电。
如图11所示为海水温差发电的开放式系统，发电系统包括一汽轮机31、一发电机32，汽轮机31上设有一新蒸汽进口和一乏蒸汽出口，汽轮机32的机轴上连接所述发电机的转子，现有技术中，设有一闪蒸器033，将通过温海水泵036将温海水导入真空状态的闪蒸器033，使其部分蒸发，其蒸气压力约为3kPa(25℃)，相当于0.03大气压力。水蒸气在低压汽轮机31内进行绝热膨胀，做完功之后排出，由冷海水泵037抽冷海水将水蒸气冷凝成液体。冷凝的方法有两种：一种是水蒸汽直接混入冷海水中，称为直接接触冷凝；另外一种是使用表面冷凝器034，水蒸汽不直接与冷海水接触。后者即是附带制备淡水的方法(见图11)。
在本发明中，将闪蒸器033换成所述真空升华蒸发机组，将从容器1中抽出并通过压气机压缩形成的蒸汽通入所述螺杆膨胀机或汽轮机。
方法1，如图13所示，运用开式循环系统的温差发电系统，结合上述实施例1，用两台 多级轴流式压气机21和22组成的真空升华蒸发机组2将从容器1中抽出的蒸汽经过压缩后直接通过螺杆膨胀机或汽轮机发电。由于蒸汽出口压力7500Pa，温度在200°以上，大大优于原有运行方案，也应有较高的发电效率。开放式循环系统不使用工作介质(工质)。
如图12所示，现有技术中海水温差发电还有一种闭式循环系统，封闭式循环系统系利用低沸点的工作流体作为工质。其主要组件包括蒸发器33、冷凝器34、涡轮机31、和发电机32，还包括工质泵035以及温海水泵036与冷海水泵037。当温海水泵将温海水抽起，并将其热源传导给蒸发器内的工质，而使其蒸发。蒸发后的工质在涡轮机内绝热膨胀，并推动涡轮机的叶片而达到发电的目的。发电后的工质被导入冷凝器，并将其热量传给抽自深层的冷海水，因而冷却并且再恢复成液体，然后经循环泵打至蒸发器，形成一个循环。工质可以反覆循环使用，其种类有氨、丁烷、氟氯烷等密度大、蒸气压力高的气体冷冻剂。以氨及氟氯烷22为最有可能的工作流体。封闭式循环系统之能源转换效率在3.3％～3.5％。若扣除泵的能源消耗，则净效率在2.1％～2.3％。
在本发明中，对加热工质的蒸发器33进行改进，将真空升华蒸发机组2中的蒸汽或冷凝水引入蒸发器33替代温海水，或者将真空升华蒸发机组2中的冷凝器23替代工质蒸发器。
方法2：如图14所示，直接将上述实施例4中的真空升华蒸发冷热能分离系统中的真空升华蒸发机组力的冷凝器23中排出的50°-70°热水引入海水温差发电系统，热水通入闭式循环系统中的蒸发器33，加热工质使其获得能量去做功。发电效率应在8％-10％。
方法3，如图15所示，将海水温差发电闭式循环系统中的蒸发器33与上述实施例4中的真空升华蒸发冷热能分离系统中的真空升华蒸发机组力的冷凝器23合并设计，用冷凝器23替代蒸发器33，在压比为15时，压力7500Pa，蒸汽出口温度200°以上，气液平衡温度41°。该工作参数大大优于海水温差发电系统3300Pa压力，25°蒸汽出口温度的条件。温差大大增加，发电效率应在15％左右，可满足商业化需求。
在上述的方法2和方法3中，工质还是通过工质泵035循环。工质的冷凝可以使用容器1中排出的冰浆。即冷凝器34中冷却剂流道直接或间接地引入容器1中排出的冰浆。
运用真空升华蒸发冷热能分离技术生产50-70°的热水(在COP＝5的条件下，成本为0.1元/KWH)。以此为能源进行发电，冷热温差可达50°以上。发电效率将达到10％。由于夏季对热能需求小，真空升华蒸发冷热能分离装置夏季分离出的热量用处不多。因而造成了近5-6月的热水能量可以很低的价格购入，用于发电。所产的电力可自用(可提高COP值，降低冷热能分离成本)也可利用峰谷电价出售，以实现效益最大化。在本发明的描述中，需要理解的是：
术语“第一”、“第二”仅用于描述目的，而不能理解为指示或暗示相对重要性或者隐 含指明所指示的技术特征的数量。由此，限定有“第一”、“第二”的特征可以明示或者隐含地包括一个或者更多个该特征。在本发明的描述中，“多个”的含义是两个或两个以上，除非另有明确具体的限定。
此外，术语“安装”、“相连”、“连接”、“固定”等术语应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或成一体；可以是机械连接，也可以是电连接，还可以是通信；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通或两个元件的相互作用关系，“连接”还可以是通过管路连接。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本发明中的具体含义。

Claims (12)

  1. 一种高效率的真空升华蒸发冷热能分离系统，其特征在于：包括一个密封的容器，在该容器上设有液体进口、气体出口和固体或固液混合物出口；在该气体出口上连接一真空升华蒸发机组，为密封容器提供设定的蒸发压力；
    所述真空升华蒸发机组为一压气机组，其包括至少一台压气机，该压气机上设有吸气口和排气口，所述吸气口与所述容器的气体出口连接。
  2. 根据权利要求1所述的高效率的真空升华蒸发冷热能分离系统，其特征在于：所述压气机组包括至少两台压气机，各台压气机串联连接；和/或，
    所述压气机是轴流式压气机；和/或，是离心式压缩机；和/或，
    所述轴流式压气机为多级轴流式压气机；和/或，
    所述真空升华蒸发机组中还包括换热器，作为冷却器和/或冷凝器，其中设置蒸汽通道和冷却剂通道，该蒸汽通道的进口与在前的所述压气机的排气口连接，以对所述压气机抽出的蒸汽冷却或冷凝；和/或，
    所述真空升华蒸发机组中还包括一真空泵，该真空泵的出口与大气连通，其入口连接在前所述压气机或冷却器或冷凝器。
  3. 根据权利要求2所述的高效率的真空升华蒸发冷热能分离系统，其特征在于：所述多级轴流式压气机是：包括一个机壳，在该机壳中设置该压气机的电机，该电机为其两端各设置一输出轴且两根输出轴同轴线的双轴电机，在两根输出轴上分别设有若干转子叶片，在相邻的转子叶片之间设置静子叶片，该静子叶片固定在所述机壳上；和/或，
    所述多级轴流式压气机为对旋式压气机，即包括两个多级轴流压气机，两个压气机的机壳密封连接，两个多级轴流压气机中的叶轮的旋向相反，电机转向相反，形成对旋效应；和/或，
    所述真空泵为螺杆式真空泵。
  4. 根据权利要求3所述的高效率的真空升华蒸发冷热能分离系统，其特征在于：
    在两根输出轴上对称地设置数量相同的转子叶片；和/或，
    在每根所述输出轴上设置2-4个所述转子叶片；和/或，
    所述多级轴流式压气机，在所述电机两侧与所述电机相邻的转子叶片的轮毂的端部内凹，电机机身两端的至少一部分容纳在内凹的空间中，在两个与电机相邻的转子叶片之间的电机机身上设置静叶片；和/或，
    在所述电机机身上设置所述静子叶片处设有冷却装置，以利于电机散热；和/或，
    该静子叶片成为所述电机在所述机壳中的支架；和/或，
    该静子叶片成为所述电机在所述机壳中的支架，在该支架上设置电源输入端口和冷却装置的输入输出端口；和/或，
    所述多级轴流式压气机机壳由一段圆锥形筒和一段圆柱形筒组成，该圆锥形筒的大直径一端为该压气机的进口端。
  5. 根据权利要求1至4之一所述的高效率的真空升华蒸发冷热能分离系统，其特征在于：所述真空升华蒸发机组为：
    包括一台多级轴流式压气机和一台真空泵，其串联连接，所述多级轴流式压气机的进气口连接所述容器的气体出口，所述真空泵的出气口与大气连通；或者，
    包括一台对旋结构的多级轴流式压气机、一台冷凝器和一台真空泵，其顺序串联连接，所述多级轴流式压气机的进气口连接所述容器的气体出口，所述真空泵的出气口与大气连通；或者，
    包括一台对旋结构的多级轴流式压气机和一台离心式压气机，其串联连接；或者，
    包括一台对旋结构的多级轴流式压气机、一台冷却器、一台压气机、一台冷凝器和一台真空泵，其顺序串联连接，其中的压气机为对旋结构的多级轴流式压气机或离心式压缩机。
  6. 使用如权利要求1至5任意一项所述的高效率的真空升华蒸发冷热能分离系统的分离方法，其特征在于：
    其中包括使用所述真空升华蒸发机组从所述容器中抽取蒸汽的步骤。
  7. 根据权利要求6所述的分离方法，其特征在于：在该抽取蒸汽的步骤中，前一个压气机抽出的蒸汽在进入下一个压气机之前先引入一冷却器或冷凝器；和/或，
    在该抽取蒸汽的步骤中，所述真空升华蒸发机组中各个压气机的压比范围在2-20；和/或，
    在该抽取蒸汽的步骤中，所述冷却器和/或冷凝器中的冷却剂为常温空气或水；或者，
    在该抽取蒸汽的步骤中，所述冷却器和/或冷凝器中的冷却剂为在后的所述冷凝器中排出的冷凝水；和/或，
    抽取蒸汽步骤中，通过二级压气机直接抽出水蒸气：第一级压气机压比：15，串联第二级压气机压比：15，总压比：225；或者，
    抽取蒸汽步骤中，第一级压气机压比：15-16，对应气液平衡压力7500Pa-8000Pa，温度40.5℃，随后，蒸汽进入串联的换热器，将70％-90％的水蒸汽冷凝为温水，之后，进入第二级压气机，其压比：15，抽出剩余的水蒸气；或者，
    抽取蒸汽步骤中，第一级压气机压比：15-16，对应气液平衡压力7500Pa-8000Pa，温度40.5℃，随后，蒸汽进入串联换热器，将70％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出 口被后面串联的螺杆真空泵抽出；或者，
    抽取蒸汽步骤中，第一级压气机压比：3-4，对应气液平衡压力1500Pa-2000Pa，温度13°-17℃，随后蒸汽进入串联冷凝器，输入的冷却介质温度2℃以下，将40％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出口被后面串联的压气机和/或螺杆真空泵抽出；或者，
    抽取蒸汽步骤中，第一级压气机压比：4，随后串联冷却器降温，再串联一台离心压缩机或轴流压气机，其压比：4，总压比为16，对应气液平衡压力7500Pa-8000Pa，温度40℃，随后，蒸汽进入串联换热器将70％-90％的水蒸汽冷凝为温水，剩余的水蒸气从冷凝器出口被后面串联的螺杆真空泵抽出；和/或，
    在所述冷凝器中将由前面的压气机抽出的蒸汽中的70-90％冷凝下来。
  8. 利用权利要求1至5其中任一项所述的高效率的真空升华蒸发冷热能分离系统进行发电方法，其中包括一发电系统，
    该发电系统包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，其特征在于：将所述真空升华蒸发机组中的蒸汽通入所述螺杆膨胀机或汽轮机；或者，
    所述发电系统包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一工质新蒸汽进口和一工质乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，还包括一工质蒸发器和一工质泠凝器，所述工质蒸发器中设有相变工质流道和加热剂流道，工质蒸发器中的相变工质流道的两端分别是液态工质进口和气态工质蒸汽出口，所述工质冷凝器中设有相变工质流道和冷却剂流道，工质冷凝器中的相变工质流道的两端分别是工质乏蒸汽进口和液态工质出口，所述工质蒸发器的气态工质蒸汽出口连接所述螺杆膨胀机或汽轮机的工质新蒸汽进口，所述螺杆膨胀机或汽轮机的乏蒸汽出口连接所述工质冷凝器的工质乏蒸汽进口，所述工质冷凝器的液态工质出口连接所述工质蒸发器的液态工质进口；其特征在于：
    在所述工质蒸发器的加热剂流道中通入所述真空升华蒸发机组中的蒸汽或热水，用以将工质加热成蒸汽通入所述螺杆膨胀机或汽轮机。
  9. 根据权利要求8所述的温差发电方法，其特征在于：
    将所述工质蒸发器中所述加热剂流道的进口连接到所述真空升华蒸发机组中所述压气机组上的排气口；或者，
    连接所述真空升华蒸发机组中所述压气机组后面连接的所述冷凝器或冷却器的出口；或者，
    将所述工质蒸发器和所述真空升华蒸发机组中的冷凝器或冷却器合二为一，压气机排出的蒸汽或热水对工质进行加热，然后再排放；和/或，
    所述工质冷凝器中所述冷却剂流道直接或间接地引入所述容器中排出的冰浆。
  10. 利用权利要求8至9其中任一项所述的发电方法中使用的发电系统，其特征在于：包括一螺杆膨胀机或汽轮机、一发电机，所述螺杆膨胀机或汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，其特征在于：所述真空升华蒸发机组中的所述压气机组的蒸汽出口连接所述螺杆膨胀机或汽轮机的所述新蒸汽进口；或者，
    利用权利要求8至9所述的发电方法中使用的发电系统，其特征在于：包括一螺杆膨胀机或汽轮机、一发电机，所述汽轮机上设有一新蒸汽进口和一乏蒸汽出口，该螺杆膨胀机或汽轮机的机轴上连接所述发电机的转子，还包括一工质蒸发器和一工质冷凝器，所述工质蒸发器中设有相变工质流道和加热剂流道，工质蒸发器中的相变工质流道的两端分别是液态工质进口和新气态工质蒸汽出口，所述工质冷凝器中设有相变工质流道和冷却剂流道，工质冷凝器中的相变工质流道的两端分别是工质乏蒸汽进口和新液态工质出口，所述工质蒸发器的新气态工质蒸汽出口连接所述螺杆膨胀机或汽轮机的蒸汽进口，所述螺杆膨胀机或汽轮机的乏蒸汽出口连接所述工质冷凝器的工质乏蒸汽进口，所述工质冷凝器的新液态工质出口连接所述工质蒸发器的液态工质进口；其特征在于：
    所述工质蒸发器的加热剂流道的进口连接所述真空升华蒸发冷热能分离系统的如下位置至少其中之一：
    所述真空升华蒸发机组中所述压气机组上的排气口；
    所述真空升华蒸发机组中所述压气机组中的所述冷凝器或冷却器的出口；
    所述真空升华蒸发机组中所述压气机的出口；
  11. 根据权利要求10所述的发电系统，其特征在于：所述工质蒸发器即为所述真空升华蒸发机组中所述压气机组中的所述冷凝器或冷却器。
  12. 根据权利要求10至11所述的发电系统，其特征在于：所述工质冷凝器的冷却剂流道的进口直接或间接连接所述容器的冰浆出口。
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