CN113753992B - High-efficiency vacuum sublimation evaporation cold and heat energy separation system and separation method and application thereof - Google Patents
High-efficiency vacuum sublimation evaporation cold and heat energy separation system and separation method and application thereof Download PDFInfo
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- CN113753992B CN113753992B CN202111145406.5A CN202111145406A CN113753992B CN 113753992 B CN113753992 B CN 113753992B CN 202111145406 A CN202111145406 A CN 202111145406A CN 113753992 B CN113753992 B CN 113753992B
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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
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- 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
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- 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
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
Abstract
The invention provides a high-efficiency vacuum sublimation evaporation cold and heat energy separation system, wherein the separation system comprises a sealed container, and a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet are arranged on the container; the gas outlet is connected with a vacuum sublimation evaporation unit to provide a set evaporation pressure for the sealed container; the vacuum sublimation evaporation unit is a compressor unit and comprises at least one compressor, an air suction port and an air exhaust port are arranged on the compressor, and the air suction port is connected with the gas outlet of the container. The invention also provides a separation method, wherein various pressure ratio designs of the compressor of the vacuum sublimation evaporation unit are given, and the separation system and the corresponding separation method can suck the water vapor generated by vacuum evaporation in the container in a large flow so as to improve the separation efficiency of cold heat energy and hot heat energy; the invention also provides a power generation method and a power generation system for generating power by using the separation system.
Description
Technical Field
The invention belongs to the technical field of green energy, relates to a vacuum sublimation evaporation cold and heat energy separation system, and particularly provides a high-efficiency vacuum sublimation evaporation cold and heat energy separation system and a separation method using the separation system. In addition, the application of the separation system in ocean thermoelectric power generation is also provided.
Background
The vacuum sublimation evaporation cold-heat energy separation technology is a technology for separating energy in water by utilizing vacuum evaporation and sublimation. The water contains a large amount of energy, and one ton of water at normal temperature of 20 ℃ can be heated to 100 ℃ by using the latent heat of crystallization released by the ice formation of one ton of water at 0 ℃, and the energy can reach 93 KWH. Compared with dam construction for power generation, the potential energy of one ton of water can only generate about 0.3KWH under the condition of over one hundred meters of height drop, and is only 0.32% of the potential energy of crystallization latent heat in one ton of water, namely the potential energy of crystallization in the same amount of water is about 290 times of the potential energy of one hundred meters of water drop. Taking the Yangtze river as an example, the three gorges dam generates about 1000 hundred million degrees of electricity each year, and the flow of the Yangtze river is approximately 10000 million tons per year. (72255 hundred million degrees of annual energy production and 10248 hundred million degrees of civil electricity in China, the three gorges generate 1.38 percent of the total national energy production by calculation). And the latent heat of crystallization contained in the water in the drainage basin is about 930000 hundred million degrees. The generated energy is only about one thousandth of the latent heat of crystallization.
Water is also a good energy storage carrier, and the adjustment of the earth temperature is well realized. Compared with the existing energy storage battery, see table 1 below:
TABLE 1
As can be seen from table 1, from the energy storage perspective only, the thermal energy (sensible heat and latent heat of crystallization) stored in 1 ton of normal temperature water is nearly three times that of the lead battery, which is 1/2 of the hottest lithium battery, and the energy storage capacity is large.
The separated energy can make the heat energy be stored in the form of hot water or steam, and the cold energy be stored in the form of ice slurry or ice blocks, and can be used. The hot water with the temperature of 35-40 ℃ can be used for production activities such as winter heating, planting and breeding of agricultural greenhouses and the like. Even in winter in northern China, the running water below the ice layer of the river still stores huge energy. The ice after separating out the heat energy can be naturally melted in proper seasons or conditions. Can provide a new production mode for a wide area with short frost-free period. The separated cold energy can be used for production activities such as ice making, air conditioning in summer (ground cooling, which can be realized by cold water at 16-18 ℃), cold source providing for agricultural product preservation and the like. The freezing method can also be used for desalting seawater and brackish water and opening up a new water source. The cold and heat energy separation technology is a green energy technology with wide application and development prospect.
The ocean thermal power generation is proposed based on the phenomenon that the temperature difference between the surface and the deep part of seawater is about 20 ℃, the principle of the ocean thermal power generation is shown in figures 11 and 12, but the ocean thermal power generation has not been commercialized for hundreds of years, and one reason is that the ocean thermal power generation is only performed by using sensible heat in seawater, so that the heat energy used by each ton of water is insufficient, the power generation efficiency is low, the seawater amount is large, and a large amount of energy is consumed for extracting the deep seawater. The cold and heat energy separation is to utilize the latent heat of liquid, so the power generation efficiency can be greatly improved and the water conveying capacity can be reduced compared with the case of only utilizing the sensible heat of the liquid, and the prior art does not have the scheme.
As shown in fig. 1, the cold-heat energy separation system comprises a sealed container 1 and a vacuum-pumping system 2 for pumping vacuum to the container 1 to form an artificial environment in which water can be evaporated under vacuum. In order to maintain a predetermined vacuum condition in the container 1 and continuously evaporate water therein to obtain an efficient effect of separating cold and heat energy, the most critical step is to efficiently extract water vapor from the artificial vacuum environment. Under the vacuum environment of 500Pa, the density of the water vapor is greatly reduced, and is about one-two hundredth of the density under the atmospheric pressure condition. Under such conditions, with the existing vacuum pump system fully utilized, the mass flow will be small, thereby making the separation inefficient.
In order to improve the efficiency of the cold-heat energy separation, a large-mass-flow vacuum-pumping system is required to be configured. How to make the vacuum-pumping system have large mass flow so as to make the cold-heat energy separation be carried out with high efficiency is the technical problem to be solved by the invention.
Disclosure of Invention
The invention aims to provide a high-efficiency vacuum sublimation evaporation cold and heat energy separation system, wherein a vacuum pumping system can pump water vapor generated by vacuum evaporation in a container in a large flow so as to improve the separation efficiency of cold and heat energy.
It is another object of the present invention to provide a separation method using the separation system.
It is a further object of the present invention to provide a system and method for generating electricity utilizing the aforementioned high efficiency vacuum sublimation evaporation cold thermal energy separation system.
The purpose of the invention is realized as follows:
a high-efficiency vacuum sublimation evaporation cold and heat energy separation system comprises a sealed container, wherein a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet are formed in the container; the gas outlet is connected with a vacuum-pumping system which is a vacuum sublimation evaporation unit and continuously and efficiently pumps out steam in the container to provide set evaporation pressure for the sealed container;
the vacuum sublimation evaporation unit is a compressor unit, which comprises at least one compressor, wherein the compressor is provided with an air suction port and an air exhaust port, and the air suction port of the compressor is connected with the gas outlet of the container.
Further, the compressor unit comprises at least two compressors, and each compressor is connected in series.
Preferably, the compressor may be an axial compressor or a centrifugal compressor.
Preferably, the axial flow compressor is a multistage axial flow compressor.
Specifically, a preferred solution for a multistage axial compressor is: the multistage axial-flow compressor comprises a shell, a motor of the compressor is arranged in the shell, the motor is a double-shaft motor with two output shafts arranged at two ends of the motor respectively and the two output shafts are coaxial, a plurality of rotor blades are fixedly arranged on the two output shafts respectively, a stator blade is arranged between the adjacent rotor blades, and the stator blade is fixed on the shell.
Preferably, the same number of rotor blades is arranged symmetrically on both output shafts.
Preferably, 2-4 said rotor blades are provided on each said output shaft.
Preferably, the end parts 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 a stationary blade is arranged on the motor body between the two rotor blades adjacent to the motor.
Preferably, a cooling device is arranged at the position where the stator blade is arranged on the motor body, so that heat dissipation of the motor is facilitated.
The stator blades become a support for the motor in the housing. The bracket is provided with a power input port and an input/output port of the cooling device.
Preferably, the multistage axial flow compressor casing is composed of a section of conical cylinder and a section of cylindrical cylinder, and the large-diameter end of the conical cylinder is the inlet end of the compressor.
Furthermore, the multistage axial-flow compressor is a contra-rotating compressor, namely, the multistage axial-flow compressor comprises two multistage axial-flow compressors, the casings of the two compressors are hermetically connected, the rotating directions of the impellers in the two multistage axial-flow compressors are opposite, and the rotating directions of the motors are opposite, so that a contra-rotating effect is formed.
Preferably, the vacuum sublimation evaporation unit further comprises a heat exchanger as a cooler and/or a condenser, wherein a steam channel and a coolant channel are provided, and an inlet of the steam channel is connected with an exhaust port of the previous compressor so as to cool or condense the steam extracted by the compressor.
Preferably, the vacuum sublimation evaporation unit further comprises a vacuum pump, an outlet of the vacuum pump is communicated with the atmosphere, and an inlet of the vacuum pump is connected to the compressor heat exchanger in front.
The following are preferred schemes for several of the vacuum sublimation evaporation units:
scheme 1: the vacuum pump comprises a multistage axial-flow compressor and a vacuum pump which are connected in series, wherein the air inlet of the multistage axial-flow compressor is connected with the air outlet of the container, and the air outlet of the vacuum pump is communicated with the atmosphere.
Scheme 2: the multi-stage axial-flow type air compressor comprises a multi-stage axial-flow type air compressor with a contra-rotating structure, a condenser and a vacuum pump, wherein the multi-stage axial-flow type air compressor, the condenser and the vacuum pump are sequentially connected in series, an air inlet of the multi-stage axial-flow type air compressor is connected with an air outlet of the container, and an air outlet of the vacuum pump is communicated with the atmosphere.
Scheme 3: the multistage axial-flow compressor comprises a multistage axial-flow compressor with a contra-rotating structure and a centrifugal compressor which are connected in series.
Scheme 4: the system comprises a multistage axial-flow compressor with a contra-rotating structure, a cooler, a compressor, a condenser and a vacuum pump which are sequentially connected in series, wherein the compressor is the multistage axial-flow compressor or the centrifugal compressor with the contra-rotating structure.
Preferably, the vacuum sublimation evaporation unit comprises more than two axial-flow compressors and a group of gas-liquid heat exchangers, namely condensers, wherein the gas-liquid heat exchangers are provided with gas inlets, gas outlets and liquid outlets, the gas inlets are connected with the exhaust ports of the first compressor, the gas outlets are connected with the gas inlets of the second compressor, and the exhaust ports of the second compressor are communicated with the atmosphere; the liquid outlet is connected with a pipeline system to collect and utilize hot water.
To improve the separation efficiency, a high-efficiency vacuum system with a large flow rate must be introduced. The axial-flow compressor or the centrifugal compressor is used as water vapor extraction equipment at an outlet of a vacuum environment, and extracted water vapor is compressed and pressurized and then introduced into the heat exchangers connected in series. The function requirement of the heat exchanger is changed from simple cooling to condensation of about 70-90% of the extracted water vapor, and condensed water at a certain temperature is directly generated. So as to obtain better heat energy separation effect.
In order to improve the reliability of the system operation and reduce the cost, the improved primary compressor and the centrifugal compressor are preferably combined into a compressor set.
Preferably, the vacuum sublimation evaporation unit further comprises a group of gas-liquid heat exchangers, namely a condenser, and a vacuum pump, wherein the condenser comprises a shell, the shell is provided with a gas inlet, a gas outlet and a liquid outlet, the gas inlet is connected with the gas outlet of the gas compressor, the gas outlet is connected with the gas inlet of the vacuum pump, and the gas outlet on the vacuum pump is communicated with the atmosphere.
The purposes of efficiently separating latent heat and sensible heat in water and achieving large-scale use are achieved through various combinations of a plurality of compressor units and a plurality of gas-liquid heat exchangers.
Preferably, the vacuum pump is a screw vacuum pump.
The invention provides a vacuum sublimation evaporation cold and heat energy separation method using the separation system, which comprises the step of extracting steam from the container by using the vacuum sublimation evaporation unit.
Further, in this step, the steam extracted by the preceding compressor is introduced into a heat exchanger, before entering the next compressor, as a cooler in which the steam extracted by the preceding compressor is cooled or a condenser in which 70 to 90% of the steam is condensed.
In the step of extracting steam, the pressure ratio of each compressor in the vacuum sublimation evaporation unit is in the range of 2-20.
The following are preferred embodiments among several steam extraction steps:
scheme 1: in the step of extracting steam, directly extracting steam through a secondary compressor: pressure ratio of the first-stage compressor: 15, connecting the second-stage compressor in series: 15, total pressure ratio: 225.
scheme 2: the water vapor is not directly drawn off, but is condensed by means of a heat exchanger.
In the step of extracting steam, the pressure ratio of a first-stage compressor is as follows: 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, the temperature of 40.5 ℃, then, the steam enters a heat exchanger connected in series, 70% -90% of the steam is condensed into warm water, and then, the warm water enters a second-stage compressor, and the pressure ratio is as follows: and 15, pumping out residual water vapor.
Scheme 3: the water vapor is not directly drawn off, but is condensed by means of a heat exchanger.
In the step of extracting steam, the pressure ratio of a first-stage compressor is as follows: 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, the temperature of 40.5 ℃, then, the steam enters a series heat exchanger, 70% -90% of the steam is condensed into warm water, and the rest steam is pumped out from the outlet of the condenser by a screw vacuum pump connected in series at the back.
Scheme 4: the water vapor is not directly drawn off, but is condensed by means of a heat exchanger.
In the step of extracting steam, the pressure ratio of a first-stage compressor is as follows: 4, then the heat exchanger is connected in series for cooling, and then a centrifugal compressor is connected in series, wherein the pressure ratio is as follows: 4, the total pressure ratio is 16, the corresponding gas-liquid equilibrium pressure is 7500Pa-8000Pa, the temperature is 40.5 ℃, then, the steam enters a series heat exchanger to condense 70% -90% of the steam into warm water, and the rest steam is pumped out from the outlet of the condenser by a screw vacuum pump connected in series at the back.
Scheme 5: the water vapor is not directly extracted, but condensed by a heat exchanger.
Pressure ratio of the first-stage compressor: 3-4, corresponding to the gas-liquid equilibrium pressure of 1500Pa-2000Pa and the temperature of 13-17 ℃, then, steam enters a series condenser, 40-90% of the steam is condensed into warm water when the temperature of the input cooling medium is below 2 ℃, and the rest steam is pumped out from the outlet of the condenser by a compressor and/or a screw vacuum pump which are connected in series later.
The method is suitable for application mainly in seawater desalination production.
In the step of extracting steam, the coolant in the cooler and/or the condenser is normal-temperature air or water, for example, air or water with the temperature of 20-30 ℃.
The coolant in the cooler and/or condenser may be condensed water discharged in the following condenser during extraction of steam.
Different process condition designs are utilized, and 70-90% of water vapor pumped by the compressor is condensed into crystal water (above 50 ℃) by a condenser before the atmospheric pressure is not reached, and the crystal water is output as heat energy. Because the steam pressure output by the compressor sets with different pressure ratios is different and the condensation temperature is also different, the invention provides a perfect process design and obtains multiple possibilities of high-efficiency energy separation.
The power generation method by utilizing the high-efficiency vacuum sublimation evaporation cold-heat energy separation system comprises a power generation system, wherein the power generation system comprises a screw expander or a steam turbine and a power generator, a new steam inlet and a spent steam outlet are arranged on the screw expander or the steam turbine, and a rotor of the power generator is connected to a shaft of the screw expander or the steam turbine, and the power generation method is characterized in that: and introducing the steam in the vacuum sublimation evaporation unit into the screw expander or the steam turbine.
The power generation system further comprises a screw expander or a steam turbine and a generator, wherein the screw expander or the steam turbine is provided with a working medium new steam inlet and a working medium exhausted steam outlet, the crankshaft of the screw expander or the steam turbine is connected with a rotor of the generator, the power generation system further comprises a working medium evaporator and a working medium condenser, a phase change working medium flow passage and a heating agent flow passage are arranged in the working medium evaporator, the two ends of the phase change working medium flow passage in the working medium evaporator are respectively provided with a liquid working medium inlet and a gaseous working medium steam outlet, the working medium condenser is provided with a phase change working medium flow passage and a cooling agent flow passage, the two ends of the phase change working medium flow passage in the working medium condenser are respectively provided with an exhausted working medium steam inlet and a liquid working medium outlet, the gaseous working medium steam outlet of the working medium evaporator is connected with the working medium new steam inlet of the screw expander or the steam turbine, and the exhausted steam outlet of the screw expander or the steam turbine is connected with the working medium exhausted steam inlet of the working medium condenser The liquid working medium outlet of the working medium condenser is connected with the liquid working medium inlet of the working medium evaporator; the method is characterized in that:
and introducing steam or hot water in the vacuum sublimation evaporation unit into a heating agent flow passage of the working medium evaporator to heat the working medium into steam and introducing the steam into the screw expander or the steam turbine.
In particular, the amount of the solvent to be used,
the inlet of the heating agent flow passage in the working medium evaporator can be connected to the exhaust port of the compressor unit in the vacuum sublimation evaporator unit;
or the outlet of the condenser or the cooler connected with the rear of the compressor unit in the vacuum sublimation evaporation unit is connected;
or the working medium evaporator and a condenser or a cooler in the vacuum sublimation evaporation unit are combined into a whole, and the steam or hot water discharged by the gas compressor heats the working medium and then is discharged.
The coolant flow channel in the working medium condenser is directly or indirectly introduced into the ice slurry discharged from the container.
The power generation system comprises:
the vacuum sublimation evaporation unit comprises a screw expander or a steam turbine and a generator, wherein the screw expander or the steam turbine is provided with a new steam inlet and a spent steam outlet, a shaft of the screw expander or the steam turbine is connected with a rotor of the generator, and a steam outlet of a compressor unit in the vacuum sublimation evaporation unit is connected with the new steam inlet of the screw expander or the steam turbine. Alternatively, the first and second liquid crystal display panels may be,
the system comprises a screw expander or a steam turbine and a generator, wherein the screw expander or the steam turbine is provided with a new steam inlet and a bled steam outlet, a rotor of the generator is connected to a machine shaft of the screw expander or the steam turbine, the system also comprises a working medium evaporator and a working medium condenser, a phase change working medium flow passage and a heating agent flow passage are arranged in the working medium evaporator, a liquid working medium inlet and a new gaseous working medium steam outlet are respectively arranged at two ends of the phase change working medium flow passage in the working medium evaporator, a phase change working medium flow passage and a cooling agent flow passage are arranged in the working medium condenser, a working medium bled steam inlet and a new liquid working medium outlet are respectively arranged at two ends of the phase change working medium flow passage in the working medium condenser, the new gaseous working medium steam outlet of the working medium evaporator is connected with the steam inlet of the steam turbine, and the steam outlet of the steam turbine is connected with the working medium bled steam inlet of the working medium condenser, the new liquid working medium outlet of the working medium condenser is connected with the liquid working medium inlet of the working medium evaporator;
an inlet of a heating agent flow passage of the working medium evaporator is connected with at least one of the following positions of the vacuum sublimation evaporation cold and heat energy separation system:
an exhaust port on the compressor unit in the vacuum sublimation evaporation unit;
an outlet of the condenser or cooler in the compressor block in the vacuum sublimation evaporation unit;
an outlet of the compressor in the vacuum sublimation evaporation unit;
the working medium evaporator is the condenser or cooler in the compressor unit in the vacuum sublimation evaporation unit.
And the inlet of the coolant flow passage of the working medium condenser is directly or indirectly connected with the ice slurry outlet of the container.
The invention provides a high-efficiency vacuum sublimation evaporation cold and heat energy separation system and a separation method, wherein a vacuum sublimation evaporation unit is a gas compressor which can be a multistage axial flow gas compressor or even a multistage axial flow gas compressor with a contra-rotating structure, and the gas compressor has larger mass flow, and the arrangement of a condenser and a cooler can pump steam with large mass flow through the design of the structure and the pressure ratio of the gas compressor in the vacuum sublimation evaporation unit, so that the aim of efficiently pumping the steam generated by vacuum sublimation evaporation from a liquid state from a container and maintaining the vacuum condition in the container can be fulfilled, and the separation of cold and heat energy can be rapidly completed. So that the energy-saving application of the cold and heat energy separation system in the aspects of seawater desalination and the like has positive influence. The working medium for power generation is heated and vaporized by utilizing steam pumped by a vacuum sublimation evaporation unit in a vacuum sublimation evaporation cold and heat energy separation system or hot water after cooling or condensation, so that ice slurry discharged by a container in the cold and heat separation system is used as a cooling agent of a condenser to liquefy the working medium, and the problems that the temperature difference of the seawater temperature difference power generation is small only by the heat energy on the surface of seawater and a large amount of seawater needs to be conveyed are well solved. The present invention will be described in detail below with reference to the accompanying drawings and examples.
Drawings
Fig. 1 is a schematic structural diagram of a vacuum sublimation evaporation cold-heat energy separation system provided by the invention.
Fig. 2 is a schematic structural diagram of a vacuum sublimation evaporation unit in the separation system of embodiment 1.
Fig. 3 is a schematic structural diagram of a vacuum sublimation evaporation unit in the separation system of embodiment 2.
Fig. 4 is a schematic structural view of a vacuum sublimation evaporation unit in the separation system of embodiment 3.
Fig. 5 is a schematic structural view of a vacuum sublimation evaporation unit in the separation system of embodiment 4.
Fig. 6 is a schematic view of a multistage axial flow compressor.
Fig. 7 is a schematic diagram of a device for adding cooling to the motor in the compressor of fig. 6.
Fig. 8 is a schematic view of a compressor having a conical shell with one end, which is modified from the cylindrical shell in the compressor shown in fig. 7.
Fig. 9 is a schematic structural diagram of a compressor with a contra-rotating structure.
Fig. 10 is a schematic structural diagram of another compressor with a contra-rotating structure.
FIG. 11 is a schematic diagram of an open cycle for power generation using seawater temperature differentials.
Fig. 12 is a schematic diagram of a closed cycle for generating power using a temperature difference of seawater.
FIG. 13 is a schematic diagram of scheme 1 for power generation using a vacuum sublimation evaporation cold thermal energy separation system.
FIG. 14 is a schematic diagram of scheme 2 for power generation using a vacuum sublimation evaporation cold thermal energy separation system.
FIG. 15 is a schematic diagram of scheme 3 for power generation using a vacuum sublimation evaporation cold thermal energy separation system.
Detailed Description
As shown in figure 1, the high-efficiency vacuum sublimation evaporation cold-heat energy separation system provided by the invention comprises a sealed container, also called as a crystallizer 1, wherein an artificial environment is formed in the crystallizer 1, a liquid inlet 11, a vapor outlet 12 and a solid-liquid mixture outlet 13 are arranged in the crystallizer 1, a vacuum sublimation evaporation unit 2 is connected to the vapor outlet 12, and a stirrer 14 is further arranged in the crystallizer 1.
The crystallizer 1 is vacuumized by the vacuum sublimation evaporation unit 2 to form a vacuum environment of the artificial environment, liquid, such as water, is input from the liquid inlet 11, the water is vaporized and sublimated in the vacuum environment in the crystallizer 1 in a vacuum manner, vaporized steam is continuously pumped out from the steam outlet 12 by the vacuum sublimation evaporation unit 2, the pumped steam is compressed by the compressor to increase the temperature of the steam pressure, the water left in the crystallizer 1 is frozen due to heat loss, and the ice slurry solid-liquid mixture is discharged from the outlet 13, thereby completing cold and heat energy separation.
The energy of water needs to be separated in an environment with an absolute pressure of 500Pa or less to achieve separation of energy. Under the condition that the outlet is at atmospheric pressure (the absolute pressure is 101320Pa), the pressure ratio can reach 203. If an axial-flow compressor vacuum system is used, water vapor in an environment of 500Pa is pumped out and discharged into the atmosphere, and the compression ratio is required to be more than 200. Under the condition, the power of the vacuum system of the axial flow compressor can be calculated according to the following formula, and the calculation formula and the result list are as follows:
1. the motor power estimation formula of the compressors with different pressure ratios is as follows:
P＝qm*Cp*T1*(π^((k-1)/k)-1)/eta/1000，
wherein:
p: motor power, qm: mass flow rate, Cp: constant specific heat, Cp k/(k-1) R2002J/kgk,
eta: adiabatic efficiency: eta is 0.8, pi: pressure ratio, COP: energy consumption ratio, T1: inlet temperature, K: specific heat ratio, K ═ 1.3, gas constant: r (J/KgK) ═ 462.
2. The outlet temperature calculation formula under different pressure ratios is as follows:
temperature difference of T1 ^ (pi ^ ((k-1)/k) -1)/eta
The compressor power values for various pressure ratios are listed in table 2.
TABLE 2
In table 2, P1 is the inlet pressure of the vacuum sublimation evaporation train, i.e. the pressure in the mold 1, P2 is the outlet pressure of the vacuum sublimation evaporation train, T1 is the temperature in the mold 1, T2 is the temperature of the outlet of the vacuum sublimation evaporation train, and P is the motor power of the vacuum sublimation evaporation train.
As can be seen from the above table, as the pressure ratio increases, the required power consumption also increases greatly, and the outlet temperature of the steam also increases greatly.
In the invention, the vacuum sublimation evaporation unit uses a large-flow compressor.
For the purpose of energy saving and high efficiency, a plurality of solutions are generated, and the following are the main ones. The following examples are given by way of illustration only and the scope of the invention is to be determined by the claims.
Example 1:
the vacuum sublimation evaporation unit 2 is formed by connecting two multistage axial-flow compressors in series, as shown in fig. 2. When the pressure ratio of the first multistage axial-flow compressor 21 is 20 (the pressure can reach 10,000Pa from 500 Pa) and the pressure ratio of the second multistage axial-flow compressor 22 is more than 10 (the pressure can reach more than 101320Pa from 10000 Pa), normal-pressure water vapor with the temperature of more than 100 ℃ can be directly separated, and heat energy separation is realized. From table 1, the power consumed by the two compressors can be found as follows: 1122KW +790KW 1912 KW. The temperature of the outlet steam is above 400 ℃, and the heat energy of the separated steam is more than that of the steam: 1335+3762 ═ 5097, COP > 2.67.
As can be seen from table 1, as the pressure ratio increases, the energy consumption increases and the COP decreases. The water vapor is directly extracted from the condition of 500Pa to reach the atmospheric pressure, and the COP is only about 2.67.
If the steam separated in example 1 is used for power generation, about 500 kw of electric power can be generated at an efficiency of 8 to 12% in the low-temperature engine. The COP of case 1 also reached around 3.6. The residual 80 percent of heat after power generation, 4000KWH, can still be continuously used. The problem with this embodiment is that the compressor with such a high pressure ratio is difficult to manufacture and is also expensive to manufacture.
Example 2:
in order to ensure good efficiency, corresponding measures are taken to improve the energy consumption ratio. As shown in fig. 3, the vacuum sublimation evaporation unit 2 still uses two multistage axial-flow compressors, but the difference is that: a condenser 23 is connected to the air outlet of the first multistage axial flow compressor 21, most of the water vapor extracted by the compressor 21 is condensed into water, and separated heat energy is obtained in the form of hot water, and the water temperature is determined to be 50-70 ℃ (the hot water can be indirectly converted into the water vapor with smaller energy consumption later). The outlet of the condenser 23 is connected to a second multistage axial compressor 22. In such a vacuum sublimation evaporation unit, if the pressure ratio of the first compressor 21 is 15-16, 70% to 90% of the extracted water vapor is condensed into water in the condenser 23, the power of the second multistage axial flow compressor is reduced to 1/7 below of the original power, and the initial calculation result of the power is: 1122KW +790/7 is 1235KW, and the heat energy of the separated water vapor is more than: 788+3762 is 4550. The COP is 3.68, from which it can be seen that adding the condenser 23 between the two compressors results in a substantial increase in efficiency.
Example 3:
as shown in fig. 4, the vacuum sublimation evaporation plant 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 with the inlet of a multistage axial-flow compressor 21, the outlet of the compressor 21 is connected with the steam inlet of a condenser 23, the steam outlet of the condenser 23 is connected with a screw vacuum pump system 24, and the outlet of the vacuum pump 24 is emptied.
Table 3 below lists data for the outlet temperature of the compressor 21 and the corresponding equilibrium pressure P2.
TABLE 3
| P2(Pa) | Gas-liquid equilibrium temperature | 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 |
When the outlet pressure of the compressor 21-1 is 7500Pa, the pressure ratio is 15, the corresponding gas-liquid equilibrium temperature is 40.5 ℃, under the pressure, the temperature of the water vapor pumped out from the crystallizer 1 by the axial flow compressor 21 is more than 40.5 ℃, the water vapor enters the condenser 23 to exchange heat with the normal temperature water in the natural state, the normal temperature water in the natural state is about 20 ℃, the water vapor releases heat and is condensed into crystal water. The temperature difference can reach about 20 ℃, and the condition of condensing 70-90% of water vapor by heat exchange can be completely met. The screw vacuum pump 24 draws out a small amount of residual water vapor in the condenser 23 for use or evacuation.
As can be seen from Table 1, when the tip pressure was 7500Pa, the pressure ratio was 15, the power was 978KW, and the screw vacuum pump power was 75KW, the total required power was 1053 KW. The separation heat energy 800+ 3762-4562 KWH and the separation heat energy calculated COP-4.33.
In embodiment 2, a vacuum pump can also be connected downstream of the second multistage axial compressor 22.
Example 4:
as shown in fig. 5, the vacuum sublimation evaporation plant 2 includes a multistage axial flow compressor 21, a cooler 25, a centrifugal compressor 26, a condenser 23, and a screw vacuum pump 24. Which are connected in series in that order. The steam outlet 12 of the crystallizer 1 is connected with the inlet of a multistage axial-flow compressor 21, the outlet of the compressor 21 is connected with the steam inlet of a cooler 26, the steam outlet of the cooler 26 is connected with the inlet of a centrifugal compressor 26, the outlet of the centrifugal compressor 26 is connected with the steam inlet of a condenser 23, the steam outlet of the condenser 23 is connected with a screw vacuum pump system 24, and the outlet of the vacuum pump 24 is emptied.
In this embodiment, the cooler 25 cools the steam but does not condense the steam, the cooled steam is re-pressurized by the centrifugal compressor 26 to 10000Pa, and then the steam enters the condenser to condense most of the steam into water, and a small amount of the steam is discharged by the screw vacuum pump 24 and vented.
A cooler is arranged between the two air compressors to reduce the temperature of steam and improve the efficiency.
According to the motor power configuration table of the gas compressor under different pressure ratio conditions and the gas-liquid balance temperature table of water under different pressures, various process paths can be designed according to specific equipment conditions, so that the equipment investment is minimum, the energy consumption ratio is highest, and the best economic benefit is obtained.
Table 4 compares the cost of obtaining heat energy from various fuels (taking heating 1 ton of water at ambient temperature to 60 c as an example).
TABLE 4
The cost of heat energy obtained by the vacuum evaporation technology is calculated to be 112.7 yuan/MWH under the conditions that the COP is 5 and the electricity price is 0.56 yuan/degree, and is basically the same as 108 yuan/MWH of the coal. If the peak-valley electricity price and the new energy technology are utilized, the electricity price can be reduced to about 0.45 yuan, and the heat energy cost of 90 yuan/MWH is obviously lower than the coal burning cost and is half of that of an air energy water heater. And the carbon dioxide emission is nearly half of that of the air energy water heater.
In each of the above embodiments of the separation system, only the thermal energy efficiency of the separation is calculated, and at the same time, ice is also generated in the crystallizer 1, ice slurry is discharged, and cold energy (40 tons of ice) for making ice is also contained, such as water melted to 0 ℃, and cold energy 40 × 93KW is released as 3720 KWH. The cold and hot energy is summed: 4322KWH +3720KWH 8042KWH, and COP 11.7.
The compressor used in the present invention may be a multistage axial flow compressor as shown in fig. 6, which is provided with an air inlet 201 and an air outlet 202, the air inlet 201 is connected with the air outlet 12 of the crystallizer 1 or with the outlet of the previous compressor, or with the outlet of the previous cooler or condenser, and the air outlet 202 is connected with the inlet of the next compressor or cooler or condenser. As shown in fig. 6, the compressor used in the previous embodiments may be of a structure: the multistage axial flow compressor comprises a casing 203, a motor 204 of the compressor is arranged in the casing 203, the motor 204 is a double-shaft motor with two output shafts arranged at two ends of the motor and the two output shafts are coaxial, a plurality of rotor blades are fixedly arranged on the two output shafts respectively, stator blades are arranged between the adjacent rotor blades, and the stator blades are fixed on the casing 203. The same number of rotor blades are symmetrically arranged on the two output shafts. As shown in fig. 6, three rotor blades a are provided on the left output shaft of the motor 204, and three rotor blades B are provided on the right output shaft of the motor 204. Between the rotor blades, stator blades C are provided. In the multistage axial-flow compressor, the moving blades with the same number are symmetrically arranged on two sides of the motor 204, so that the two sides are balanced in power, the motor is arranged in the middle, and the stationary blades are arranged in the casing at the position of the motor, so that the structure of the compressor is more compact. In addition, the motor shaft and two rotor blades close to the motor 204 have the end parts of the hub recessed, and a part of the two ends of the motor body is accommodated in the recessed space, that is, the hub part of the blade connected with the motor shaft is arranged on the output shaft, but the blade extends out of the shell of the motor, so that the compressor is also compact. A gap is provided between the motor casing and the adjacent rotor blade.
In the middle of the shell of the motor 204, a stator blade is arranged, the stator blade can also play a role of a bracket for supporting the motor, and the axial length of the stator blade can be longer than that of other stator blades, so that the motor can be fixed in the shell of the compressor more stably.
In a better example, four rotor blades are symmetrically and fixedly arranged on the output shafts on two sides of the motor respectively.
In addition, as shown in fig. 7, an accommodating cavity may be provided inside the stator blade C1 in the middle of the motor casing, and a coil C2 is provided therein, and both ends of the coil C2 extend out of the compressor casing (not shown) along the stator blade, and are connected with a coolant to cool the motor.
In order to improve the compressing effect of the multistage axial flow compressor, as shown in fig. 8, the casing of the multistage axial flow compressor is composed of a section of conical cylinder 203-1 and a section of cylindrical cylinder 203-2, and the large-diameter end of the conical cylinder is the inlet end 201 of the compressor.
In order to obtain a higher pressure ratio, a multistage axial flow compressor may employ a counter-rotating structure. As shown in fig. 9, two multi-stage axial flow compressors as shown in fig. 6 and 7 are connected end to end, however, the rotation direction of the impeller in the latter compressor is opposite to that of the former compressor, and the rotation direction of the motor is opposite during operation. The multistage axial-flow compressor with the contra-rotating structure can achieve a pressure ratio of 16-20 by multistage series connection.
As shown in fig. 10, two compressor heads with flaring cone barrels at inlet sections may be connected end to form a multi-stage axial flow compressor with a contra-rotating structure. In each of the above embodiments, the separation method using the separation system includes a step of extracting vapor from the vessel using the vacuum sublimation evaporator unit, in which the vapor extracted from the previous compressor is introduced into a heat exchanger, i.e., a condenser, in which 70 to 90% of the vapor is condensed before entering the next compressor.
The heat exchanger is added, and the pressure ratio of each compressor in the vacuum sublimation evaporation unit is 2-20 in the process of extracting steam; for example, the pressure ratio can be reduced to 2, and the pressure ratio of each stage or each compressor can be lower by using a plurality of stages of compressors or a plurality of compressors connected in series, while the energy consumption of the whole vacuum sublimation evaporation unit is reduced, and the COP value is greatly improved.
In the process of extracting steam, the coolant in the heat exchanger is normal-temperature air or water. The number of stages or compressors is reasonably arranged, the temperature of the extracted steam can be higher than that of water or air at room temperature, and the temperature difference can be cooled by water or air at room temperature, so that the process can be conveniently carried out at low cost.
During the steam extraction process, the coolant in the heat exchanger is condensed water extracted by a subsequent heat exchanger. By reasonably designing the pressure ratio of each stage of the compressor, the condensed water of the rear heat exchanger can be directly used as the coolant of the front heat exchanger. This also increases the temperature of the coolant, thereby allowing the condensate to be reused, for example, for low temperature power generation.
A cooler can also be arranged between the two compressors, namely, in the cooler, the steam is only cooled without being condensed, so that the vacuumizing efficiency can also be improved.
The high-efficiency vacuum sublimation evaporation cold-heat energy separation system provided by the invention can also be used for power generation.
As shown in fig. 11, the open system for seawater thermoelectric power generation includes a steam turbine 31, a generator 32, a new steam inlet and a exhausted steam outlet are provided on the steam turbine 31, a rotor of the generator is connected to a shaft of the steam turbine 32, in the prior art, a flash evaporator 033 is provided, warm seawater is introduced into a flash evaporator 033 in a vacuum state by a warm seawater pump 036, so as to be partially evaporated, and the steam pressure is about 3kPa (25 ℃), which is equivalent to 0.03 atm. The steam is adiabatically expanded in the low pressure turbine 31, and is discharged after performing work, and the cold seawater is pumped by the cold seawater pump 037 to condense the steam into liquid. There are two methods of condensation: one is that the water vapor is directly mixed into cold seawater, which is called direct contact condensation; another is to use a surface condenser 034, where the water vapor does not directly contact the cold seawater. The latter method is a method for additionally preparing fresh water (see fig. 11).
In the present invention, the flash evaporator 033 is replaced with the vacuum sublimation evaporator unit, and the vapor extracted from the container 1 and compressed by the compressor is introduced into the screw expander or the steam turbine.
In the method 1, as shown in fig. 13, a thermoelectric power generation system of an open cycle system is used, and in combination with the above embodiment 1, a vacuum sublimation evaporation unit 2 composed of two multistage axial- flow compressors 21 and 22 compresses steam extracted from a container 1 and then directly generates power through a screw expander or a steam turbine. The steam outlet pressure is 7500Pa, the temperature is above 200 ℃, which is greatly superior to the original operation scheme, and the power generation efficiency is also higher. The open circulation system does not use a working medium (working fluid).
As shown in fig. 12, the seawater thermoelectric power generation in the prior art also has a closed circulation system, which uses a working fluid with a low boiling point as a working medium. The main components of the device comprise an evaporator 33, a condenser 34, a turbine 31, a generator 32, a working medium pump 035, a warm seawater pump 036 and a cold seawater pump 037. When the warm sea water pump pumps up warm sea water, the heat source of the warm sea water is conducted to the working medium in the evaporator, so that the warm sea water is evaporated. The evaporated working medium is adiabatically expanded in the turbine and pushes the blades of the turbine to achieve the purpose of generating power. The working medium after power generation is introduced into the condenser, and the heat of the working medium is transferred to cold seawater pumped from the deep layer, so that the working medium is cooled and recovered into liquid, and then the liquid is pumped to the evaporator through the circulating pump to form a cycle. The working medium can be repeatedly recycled, and the working medium can be gas refrigerant with high density and high vapor pressure, such as ammonia, butane, fluorochloroalkane and the like. Ammonia and fluorochloroalkane 22 are the most likely working fluids. The energy conversion efficiency of the closed circulation system is 3.3% -3.5%. The net efficiency is between 2.1% and 2.3% when the energy consumption of the pump is deducted.
In the invention, the evaporator 33 for heating the 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 warm seawater, or the condenser 23 in the vacuum sublimation evaporation unit 2 replaces the working medium evaporator.
The method 2 comprises the following steps: as shown in fig. 14, the hot water of 50 ° to 70 ° discharged from the condenser 23 of the vacuum sublimation evaporation unit in the vacuum sublimation evaporation cold and heat energy separation system in the above embodiment 4 is directly introduced into the seawater temperature difference power generation system, and the hot water is introduced into the evaporator 33 in the closed circulation system to heat the working medium to obtain energy to do work. The generating efficiency is 8-10%.
In the method 3, as shown in fig. 15, the evaporator 33 in the closed circulation system for seawater thermoelectric power generation is combined with the condenser 23 of the vacuum sublimation evaporator unit in the vacuum sublimation evaporation cold and heat energy separation system in the above embodiment 4, and the condenser 23 is used to replace the evaporator 33, and when the pressure ratio is 15, the pressure is 7500Pa, the vapor outlet temperature is above 200 ℃, and the vapor-liquid equilibrium temperature is 41 ℃. The working parameters are greatly superior to the conditions of 3300Pa pressure of the seawater temperature difference power generation system and 25 ℃ steam outlet temperature. The temperature difference is greatly increased, the generating efficiency is about 15 percent, and the commercialized demand can be met.
In the above-described methods 2 and 3, the working medium is again circulated by the working medium pump 035. The condensation of the working substance can be carried out using the ice slurry discharged from the vessel 1. I.e. the coolant flow channels in the condenser 34, are directly or indirectly led to the ice slurry discharged from the vessel 1.
Hot water with the temperature of 50-70 ℃ is produced by using a vacuum sublimation evaporation cold-heat energy separation technology (under the condition that COP is 5, the cost is 0.1 yuan/KWH). The temperature difference between cold and hot can reach more than 50 degrees. The generating efficiency reaches 10%. Because the demand for heat energy is small in summer, the heat energy separated by the vacuum sublimation evaporation cold-heat energy separating device in summer is not used much. Therefore, the hot water energy of 5-6 months can be purchased at a low price for generating electricity. The generated electricity can be used by oneself (COP value can be increased, cold and heat energy separation cost can be reduced), and the electricity price can be sold by utilizing peak valley electricity price, so that the benefit maximization is realized. In the description of the present invention, it is to be understood that:
the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
In addition, the terms "mounted," "connected," "fixed," and the like are to be construed broadly and may include, for example, fixed connections, detachable connections, or integral parts; the connection can be mechanical connection, electrical connection or communication; the two components can be directly connected or indirectly connected through an intermediate medium, and can be communicated with each other inside the two components or mutually interacted with each other, and the two components can be connected through a pipeline. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Claims (15)
1. A high-efficiency separation method of a vacuum sublimation evaporation cold-heat energy separation system is characterized in that:
comprising the step of extracting vapor from a sealed container using a vacuum sublimation evaporation unit,
the sealed container is provided with a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet; the gas outlet is connected with the vacuum sublimation evaporation unit to provide set evaporation pressure for the sealed container;
the vacuum sublimation evaporation unit is a compressor unit and comprises at least one compressor, the compressor is provided with an air suction port and an air exhaust port, and the air suction port is connected with the gas outlet of the container;
the compressor is an axial flow compressor; the axial-flow compressor is a multistage axial-flow compressor;
in the step of extracting the steam, the pressure ratio of each compressor in the vacuum sublimation evaporation unit is in the range of 4-20;
in the step of extracting steam, the steam extracted by the previous compressor is introduced into a heat exchanger to be used as a cooler or a condenser before entering the next compressor or a vacuum pump.
2. The separation method according to claim 1, characterized in that:
in the step of extracting steam, extracting water vapor through a secondary compressor: the first compressor has a pressure ratio: 15, connecting a second compressor in series: 15, total pressure ratio: 225, a step of mixing; alternatively, the first and second electrodes may be,
in the step of extracting steam, the pressure ratio of a first compressor is as follows: 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, the temperature of 40.5 ℃, then, the steam enters a series heat exchanger, 70% -90% of the steam is condensed into warm water, and the rest steam is pumped out from the outlet of the condenser by a screw vacuum pump connected in series at the back; alternatively, the first and second liquid crystal display panels may be,
in the step of extracting steam, the pressure ratio of a first compressor is as follows: 3-4, corresponding to the gas-liquid equilibrium pressure of 1500Pa-2000Pa and the temperature of 13-17 ℃, then feeding the steam into a series condenser, condensing 40-90% of the steam into warm water when the temperature of the input cooling medium is below 2 ℃, and pumping the rest steam out of the outlet of the condenser by a compressor and/or a screw vacuum pump connected in series later.
3. The separation method according to claim 1, characterized in that:
in the step of extracting steam, the coolant in the cooler and/or the condenser is normal-temperature air or water; alternatively, the first and second electrodes may be,
in the step of extracting steam, the coolant in the cooler and/or the condenser is condensed water discharged in the following condenser.
4. The separation method according to claim 1, characterized in that:
in the step of extracting steam, the pressure ratio of a first compressor is as follows: 15-16, corresponding to the gas-liquid equilibrium pressure of 7500Pa-8000Pa, the temperature of 40.5 ℃, then, the steam enters the serially connected cooler and/or condenser, 70% -90% of the steam is condensed into warm water, and then, the warm water enters the second compressor, and the pressure ratio is as follows: 15, pumping out the residual water vapor; alternatively, the first and second liquid crystal display panels may be,
in the step of extracting steam, the pressure ratio of a first compressor is as follows: 4, then serially connecting a cooler for cooling, and serially connecting a centrifugal compressor or an axial flow compressor, wherein the pressure ratio is as follows: 4, the total pressure ratio is 16, the corresponding gas-liquid equilibrium pressure is 7500Pa-8000Pa, the temperature is 40 ℃, then, the steam enters a series heat exchanger to condense 70% -90% of the steam into warm water, and the rest steam is pumped out from the outlet of the condenser by a screw vacuum pump connected in series at the back.
5. The separation method according to claim 1, characterized in that: in which 70-90% of the steam extracted by the preceding compressor is condensed.
6. A high-efficiency vacuum sublimation evaporation cold thermal energy separation system used in the separation method according to any one of claims 1 to 5, characterized in that: comprises a sealed container, wherein the container is provided with a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet; the gas outlet is connected with a vacuum sublimation evaporation unit to provide a set evaporation pressure for the sealed container;
the vacuum sublimation evaporation unit is a gas compressor unit and comprises at least one gas compressor, wherein the gas compressor is provided with a gas suction port and a gas exhaust port, and the gas suction port is connected with a gas outlet of the container;
the compressor is an axial flow compressor; the axial-flow compressor is a multistage axial-flow compressor;
the vacuum sublimation evaporation unit also comprises a heat exchanger which is used 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 with the exhaust port of the compressor in front so as to cool or condense the steam pumped by the compressor;
the vacuum sublimation evaporation unit also comprises a gas compressor or a vacuum pump, wherein the outlet of the gas compressor or the vacuum pump is communicated with the atmosphere, and the inlet of the gas compressor or the vacuum pump is connected with the cooler or the condenser in front.
7. The high efficiency vacuum sublimation evaporation cold thermal energy separation system of claim 6, wherein: the multistage axial-flow compressor is: the motor is a double-shaft motor with two output shafts arranged at two ends of the motor respectively and two output shafts are coaxial, a plurality of rotor blades are arranged on the two output shafts respectively, and a stator blade is arranged between the adjacent rotor blades and fixed on the shell; and/or the presence of a gas in the atmosphere,
the multistage axial-flow compressor is a contra-rotating compressor, namely comprises two multistage axial-flow compressors, the casings of the two compressors are hermetically connected, the rotating directions of impellers in the two multistage axial-flow compressors are opposite, and the rotating directions of motors are opposite, so that a contra-rotating effect is formed.
8. The high efficiency vacuum sublimation evaporation cold thermal energy separation system of claim 6, wherein: the vacuum pump is a screw type vacuum pump.
9. A high efficiency vacuum sublimation evaporation cold thermal energy separation system according to claim 7, wherein:
the rotor blades with the same number are symmetrically arranged on the two output shafts; and/or the presence of a gas in the gas,
providing 2-4 said rotor blades on each said output shaft; and/or the presence of a gas in the atmosphere,
the multistage axial-flow compressor is characterized in that the end parts of the hubs of the rotor blades adjacent to the motor on the two sides of the motor are recessed, at least one part of the two ends of the motor body is accommodated in the recessed space, and a stationary blade is arranged on the motor body between the two rotor blades adjacent to the motor; and/or the presence of a gas in the gas,
a cooling device is arranged at the position where the stator blade is arranged on the motor body, so that the heat dissipation of the motor is facilitated; and/or the presence of a gas in the atmosphere,
the stator blade becomes a support of the motor in the casing; and/or the presence of a gas in the atmosphere,
the stator blade becomes a bracket of the motor in the shell, and a power supply input port and an input/output port of the cooling device are arranged on the bracket; and/or the presence of a gas in the gas,
the multistage axial-flow compressor casing consists of a section of conical cylinder and a section of cylindrical cylinder, and the large-diameter end of the conical cylinder is the inlet end of the compressor.
10. A high efficiency vacuum sublimation evaporation cold thermal energy separation system according to one of claims 6 to 9, wherein: the vacuum sublimation evaporation unit comprises:
the multi-stage axial-flow type air compressor comprises a multi-stage axial-flow type air compressor with a contra-rotating structure, a condenser and a vacuum pump, wherein the multi-stage axial-flow type air compressor, the condenser and the vacuum pump are sequentially connected in series, an air inlet of the multi-stage axial-flow type air compressor is connected with an air outlet of the container, and an air outlet of the vacuum pump is communicated with the atmosphere;
alternatively, the first and second electrodes may be,
the system comprises a multistage axial-flow compressor with a contra-rotating structure, a cooler, a compressor, a condenser and a vacuum pump which are sequentially connected in series, wherein the compressor is the multistage axial-flow compressor or the centrifugal compressor with the contra-rotating structure.
11. A method of generating electricity using the high-efficiency vacuum sublimation evaporation cold-thermal energy separation method according to any one of claims 1 to 5, comprising an electricity generation system,
the power generation system comprises a screw expander or a steam turbine and a power generator, wherein the screw expander or the steam turbine is provided with a new steam inlet and a exhausted steam outlet, a shaft of the screw expander or the steam turbine is connected with a rotor of the power generator, and steam in the vacuum sublimation evaporation unit is introduced into the screw expander or the steam turbine; alternatively, the first and second liquid crystal display panels may be,
the power generation system comprises a screw expander or a steam turbine and a generator, wherein the screw expander or the steam turbine is provided with a working medium new steam inlet and a working medium exhausted steam outlet, the shaft of the screw expander or the steam turbine is connected with the rotor of the generator, the power generation system also comprises a working medium evaporator and a working medium condenser, the working medium evaporator is internally provided with a phase change working medium runner and a heating agent runner, two ends of the phase change working medium runner in the working medium evaporator are respectively provided with a liquid working medium inlet and a liquid working medium steam outlet, the working medium condenser is internally provided with a phase change working medium runner and a cooling agent runner, two ends of the phase change working medium runner in the working medium condenser are respectively provided with a working medium exhausted steam inlet and a liquid working medium outlet, the gaseous working medium steam outlet of the working medium evaporator is connected with the working medium new steam inlet of the screw expander or the steam turbine, and the exhausted steam outlet of the screw expander or the steam turbine is connected with the working medium exhausted steam inlet of the working medium condenser, the liquid working medium outlet of the working medium condenser is connected with the liquid working medium inlet of the working medium evaporator,
the method is characterized in that: the high-efficiency vacuum sublimation evaporation heat energy separation method of any one of claims 1 to 5 is used for generating steam or hot water, and the steam or hot water in the vacuum sublimation evaporation unit is introduced into a heating agent flow passage of the working medium evaporator so as to heat the working medium into steam and introduce the steam into the screw expander or the steam turbine.
12. A method of generating electricity according to claim 11, wherein:
connecting an inlet of the heating agent flow channel in the working medium evaporator to an exhaust port on the compressor unit in the vacuum sublimation evaporation unit; alternatively, the first and second liquid crystal display panels may be,
the outlet of the condenser or the cooler connected with the rear of the compressor unit in the vacuum sublimation evaporation unit is connected; alternatively, the first and second electrodes may be,
combining the working medium evaporator and a condenser or a cooler in the vacuum sublimation evaporation unit into a whole, heating the working medium by steam or hot water discharged by the gas compressor, and then discharging; and/or the presence of a gas in the atmosphere,
the coolant flow channel in the working medium condenser is directly or indirectly introduced into the ice slurry discharged from the container.
13. A power generation system for use in a power generation method according to any one of claims 11 to 12, characterized in that: the high-efficiency vacuum sublimation evaporation cold and heat energy separation system comprises the high-efficiency vacuum sublimation evaporation cold and heat energy separation system as claimed in any one of claims 6 to 10, a screw expander or a steam turbine, and a generator, wherein the screw expander or the steam turbine is provided with a new steam inlet and a spent steam outlet, a shaft of the screw expander or the steam turbine is connected with a rotor of the generator, and a steam outlet of the compressor unit in the vacuum sublimation evaporation unit is connected with the new steam inlet of the screw expander or the steam turbine; alternatively, the first and second electrodes may be,
the high-efficiency vacuum sublimation evaporation cold and heat energy separation system comprises the high-efficiency vacuum sublimation evaporation cold and heat energy separation system, a screw expander or a steam turbine and a generator, wherein the steam turbine is provided with a new steam inlet and a spent steam outlet, the shaft of the screw expander or the steam turbine is connected with the rotor of the generator, the high-efficiency vacuum sublimation evaporation cold and heat energy separation system further comprises a working medium evaporator and a working medium condenser, the working medium evaporator is internally provided with a phase-change working medium flow passage and a heating agent flow passage, the two ends of the phase-change working medium flow passage in the working medium evaporator are respectively provided with a liquid working medium inlet and a new gaseous working medium steam outlet, the working medium condenser is internally provided with a phase-change working medium flow passage and a cooling agent flow passage, the two ends of the phase-change working medium flow passage in the working medium condenser are respectively provided with a working medium spent steam inlet and a new liquid working medium outlet, and the new gaseous working medium steam outlet of the working medium evaporator is connected with the steam inlet of the screw expander or the steam turbine, a bled steam outlet of the screw expander or the steam turbine is connected with a working medium bled steam inlet of the working medium condenser, and a new liquid working medium outlet of the working medium condenser is connected with a liquid working medium inlet of the working medium evaporator;
the inlet of the heating agent flow passage of the working medium evaporator is connected with at least one of the following positions of the vacuum sublimation evaporation cold and heat energy separation system:
an exhaust port on the compressor unit in the vacuum sublimation evaporation unit;
an outlet of the condenser or cooler in the compressor block in the vacuum sublimation evaporation unit;
and the outlet of the compressor in the vacuum sublimation evaporation unit.
14. The power generation system of claim 13, wherein: the working medium evaporator is the condenser or the cooler in the compressor unit in the vacuum sublimation evaporation unit.
15. The power generation system according to any one of claims 13 to 14, wherein: and the inlet of the coolant flow channel of the working medium condenser is directly or indirectly connected with the ice slurry outlet of the container.
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| CN113753992B (en) * | 2021-09-07 | 2022-07-22 | 武伟 | High-efficiency vacuum sublimation evaporation cold and heat energy separation system and separation method and application thereof |
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| CN112983783A (en) * | 2021-03-30 | 2021-06-18 | 北京理工大学 | Energy storage subsystem applied to compressed air energy storage system and operation method |
| CN113753992B (en) * | 2021-09-07 | 2022-07-22 | 武伟 | High-efficiency vacuum sublimation evaporation cold and heat energy separation system and separation method and application thereof |
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2021
- 2021-09-28 CN CN202111145406.5A patent/CN113753992B/en active Active
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| WO2023036066A1 (en) | 2023-03-16 |
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