CN113087054A - Low temperature evaporation system - Google Patents

Abstract

The invention relates to a low-temperature evaporation system. The low-temperature evaporation system comprises a separation chamber, a heater and an air compressor; the air compressor is connected with the heater to supply primary steam with the temperature of 45-65 ℃ to the heater; the separation chamber is connected with the heater, the stock solution is evaporated in the separation chamber to form circulating liquid, the circulating liquid exchanges heat with the primary steam in the heater to be heated to 40-60 ℃, then flows into the separation chamber with the internal pressure of 0.03-0.04 MPa to be evaporated, and circularly flows between the separation chamber and the heater to be gradually concentrated. This system is through utilizing the low temperature steam that the air compressor machine produced to carry out circulation heating to the circulating liquid in the separator to make the circulating liquid maintain in lower temperature, and concentrate step by step in the separator, not only can ensure going on smoothly of stoste low temperature evaporation process, also make whole vaporization system with this state continuous stable work moreover, and need not frequent switching on and shutting down, reduce the energy consumption when reducing the equipment loss.

Description

Low temperature evaporation system

Technical Field

The invention relates to the technical field of sewage treatment equipment, in particular to a low-temperature evaporation system.

Background

The existing common evaporation system is generally high in temperature when performing evaporation treatment on sewage, and for some sewage which is small in treatment capacity and requires to be evaporated at a low temperature, the common evaporation system can only be stopped after being started for a period of time, so that the sewage is evaporated after the temperature is gradually reduced to the required low temperature. However, this mode of operation not only results in equipment losses due to frequent switching on and off of the conventional vaporization system, but also results in increased energy consumption due to heat loss that occurs when the conventional vaporization system is lowered from a high temperature to a low temperature.

Disclosure of Invention

Based on this, there is a need for a cryogenic vaporization system.

A low-temperature evaporation system comprises a separation chamber, a heater and an air compressor; the air compressor is connected with the heater to supply primary steam with the temperature of 45-65 ℃ to the heater; the separation chamber is connected with the heater, the stock solution is evaporated in the separation chamber to form circulating liquid, the circulating liquid exchanges heat with the primary steam in the heater to be heated to 40-60 ℃, then flows into the separation chamber with the internal pressure of 0.03-0.04 MPa to be evaporated, and circularly flows between the separation chamber and the heater to be gradually concentrated.

Among the above-mentioned low temperature vaporization system, through the low temperature steam that utilizes the air compressor machine to produce to carry out circulation heating to the circulating liquid in the separator chamber to make the circulating liquid maintain in lower temperature, and concentrate step by step in the separator chamber, not only can ensure going on smoothly of stoste low temperature evaporation process, but also make whole vaporization system carry out continuous stable work with this state, and need not frequent switching on and shutting down, reduce the energy consumption when reducing the equipment loss.

In one embodiment, the low-temperature evaporation system comprises a condenser, the condenser is connected with the separation chamber, secondary steam generated by evaporation in the separation chamber exchanges heat with stock solution in the condenser to reduce the temperature, and the heated stock solution enters the separation chamber. Through setting up the condenser, the secondary steam that makes the evaporation produce in the separator exchanges heat at condenser and stoste to make the stoste that lets in the separator heat up, not only can make the heat that secondary steam carried obtain utilizing, reduce the calorific loss of system, can also reduce the circulation liquid and to the thermal utilization of primary steam, reduce the energy consumption of air compressor machine.

In one embodiment, the secondary steam generated by evaporation in the separation chamber is cooled to 35-45 ℃ after heat exchange between the condenser and the stock solution.

In one embodiment, the low-temperature evaporation system comprises a liquid storage tank connected with the condenser, and the liquid storage tank can collect distilled water obtained by condensing secondary steam in the condenser.

In one embodiment, the low-temperature evaporation system comprises a heat exchanger, the heat exchanger is connected with the heater, the separation chamber and the air compressor, and primary steam discharged by the heater exchanges heat with secondary steam generated by evaporation in the separation chamber in the heat exchanger; the temperature of the primary steam after heat exchange is increased, and the primary steam can enter the air compressor to be reused. Through setting up the heat exchanger, can make primary steam absorb the heat of secondary steam and heat up, so can make the heat that secondary steam carried obtain the utilization, reduce the calorific loss of system, and simultaneously, primary steam gets into air compressor machine 13 once more after the heat transfer and is utilized, not only can make primary steam obtain recycling, and therefore the cost is reduced, and primary steam has carried certain heat, after getting into the air compressor machine, the air compressor machine only need exert less energy to it again and can satisfy the use of heater, thereby reduce the energy consumption of air compressor machine.

In one embodiment, the low-temperature evaporation system comprises a cooling structure, and the cooling structure is connected between the heat exchanger and the heater to reduce the pressure and temperature of the primary steam discharged by the heater.

In one embodiment, the cooling structure cools primary steam at 35-45 ℃ discharged by the heater to 10-20 ℃, and the temperature of the primary steam is increased to 25-35 ℃ after the primary steam and secondary steam exchange heat after the primary steam and the secondary steam are introduced into the heat exchanger.

In one embodiment, the cooling structure comprises a cooling fan and an expansion valve, and the heater, the cooling fan, the expansion valve and the heat exchanger are connected in sequence; the cooling fan carries out primary cooling on the primary steam discharged by the heater; and the expansion valve is used for carrying out pressure reduction and temperature reduction on the primary steam cooled by the cooling fan again.

In one embodiment, the cryogenic evaporation system comprises a vacuum pump connected with the heat exchanger and a separation tank connected with the vacuum pump; and discharging the secondary steam subjected to heat exchange at the heat exchanger to the separation tank under the action of the vacuum pump, and discharging the secondary steam through the separation tank.

In one embodiment, at least one of the following schemes is also included:

the air compressor is a turbine compressor;

the low-temperature evaporation system further comprises a forced circulation pump, and the forced circulation pump is connected between the heater and the separation chamber so as to make a circulating liquid forcibly circulate between the separation chamber and the heater;

the low-temperature evaporation system comprises a stock solution delivery pump, and stock solution is delivered to the separation chamber under the action of the stock solution delivery pump;

the low-temperature evaporation system comprises a liquid discharge pump connected with the separation chamber, circulating liquid in the separation chamber is concentrated step by step to form concentrated liquid, and the concentrated liquid is forcibly discharged from the separation chamber by the liquid discharge pump.

Drawings

Fig. 1 is a schematic structural diagram of a low-temperature evaporation system according to an embodiment of the present invention.

Detailed Description

In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be considered limiting of the invention.

Furthermore, 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 implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

It will be understood that when an element is referred to as being "secured to" or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like as used herein are for illustrative purposes only and do not denote a unique embodiment.

As shown in fig. 1, a low-temperature evaporation system 10 according to an embodiment of the present invention is used for performing evaporation concentration treatment on sewage at a low temperature. The low temperature evaporation system 10 includes a separation chamber 11, a heater 12, and an air compressor 13. The air compressor 13 is used for compressing and heating air to obtain high-pressure and low-temperature primary steam, and specifically, the temperature of the primary steam is 45-65 ℃. An air compressor 13 is connected to the heater 12 to supply low-temperature primary steam into the heater 12. The raw liquid (i.e. waste water) can be evaporated at a lower temperature after entering the separation chamber 11 and concentrated to form a circulating liquid. The separation chamber 11 is connected with a heater 12, circulating liquid in the separation chamber 11 can enter the heater 12, and exchanges heat with primary steam introduced into the heater 12 by an air compressor 13 in the heater 12 to raise the temperature. And the circulating liquid returns to the separation chamber 11 after the temperature is raised to the required temperature of 40-60 ℃, the pressure in the separation chamber 11 is 0.03-0.04 MPa, and the saturated evaporation pressure of water in the circulating liquid is higher than the pressure in the separation chamber 11 so as to be evaporated, so that the circulating liquid is further concentrated, and the circulating liquid is circulated for multiple times between the separation chamber 11 and the heater 12 to achieve step-by-step concentration, and is finally discharged after the concentration degree is higher.

In the low-temperature evaporation system 10, the circulating liquid in the separation chamber 11 is circularly heated by the low-temperature primary steam generated by the air compressor 13, so that the circulating liquid is maintained at a lower temperature and is gradually concentrated in the separation chamber 11, smooth running of the low-temperature evaporation process of the raw liquid can be ensured, the whole evaporation system continuously and stably works in the state, frequent startup and shutdown are not needed, and energy consumption is reduced while equipment loss is reduced.

In the embodiment shown in fig. 1 in particular, the air compressor 13 is a turbo compressor. The turbocompressor ensures that the low-temperature evaporation system 10 can efficiently complete evaporation and concentration of the wastewater in a low-temperature environment, and has an energy-saving effect.

In some embodiments, the cryogenic evaporation system 10 comprises a forced circulation pump 14, the forced circulation pump 14 being connected between the heater 12 and the separation chamber 11 to forcibly circulate the circulating liquid between the separation chamber 11 and the heater 12. By providing the forced circulation pump 14 to provide power for circulating the circulating liquid, circulation of the circulating liquid between the separation chamber 11 and the heater 12 is made possible. Specifically, as shown in fig. 1, a forced circulation pump 14 is connected between the outlet of the separation chamber 11 and the inlet of the heater 12 so as to be able to act on the circulating liquid before the heater 12 heats. The connection on the inlet side of the heater 12 prevents the forced circulation pump 14 from being at a higher operating ambient temperature than the connection of the forced circulation pump 14 on the outlet side of the heater 12, extending the life of the forced circulation pump 14.

Specifically, the stock solution introduced into the separation chamber 11 is gradually concentrated until a viscous concentrated solution with a concentration degree of 95% or more is obtained, and the concentrated solution is discharged to the outside and finally treated in a waste or buried manner. In some embodiments, the cryogenic evaporation system 10 includes a drain pump 15 connected to the separation chamber 11, the circulating liquid in the separation chamber 11 forms a concentrated liquid after being concentrated in stages, and the drain pump 15 forcibly discharges the concentrated liquid from the separation chamber 11. The concentrated liquid can be smoothly discharged from the separation chamber 11 by the power of the drain pump 15.

As shown in fig. 1, in the present embodiment, the low temperature evaporation system 10 includes a condenser 16, the condenser 16 is connected to the separation chamber 11, the secondary steam generated by evaporation in the separation chamber 11 exchanges heat with the raw liquid in the condenser 16 to reduce the temperature, and the heated raw liquid enters the separation chamber 11. So, the secondary steam that the evaporation produced in the separation chamber 11 further heats the stoste to the stoste that makes to let in the separation chamber 11 intensifies, not only can make the heat that secondary steam carried obtain utilizing, reduces the calorific loss of system, can also reduce the thermal utilization of circulation liquid to primary steam, reduces the energy consumption of air compressor machine 13. Specifically, the separation chamber 11 is evaporated to generate secondary steam of 40-60 ℃, and the secondary steam is cooled to 35-45 ℃ after exchanging heat with the stock solution in the condenser 16. It can be understood that the discharged secondary steam still carries heat after heat exchange with the stock solution.

Specifically, the low temperature evaporation system 10 includes a liquid storage tank 17 connected to the condenser 16, and the liquid storage tank 17 is capable of collecting distilled water condensed from the secondary steam in the condenser 16. It can be understood that the secondary steam generated by evaporation in the separation chamber 11 is condensed after the condenser 16 exchanges heat with the stock solution, part of the secondary steam is condensed into distilled water and collected by the stock solution tank 17, and part of the secondary steam is uncondensed non-condensable gas which carries heat and is discharged. Further, a distilled water pump 18 is connected to one side of the liquid storage tank 17 far away from the condenser 16, and the distilled water pump 18 can pump out the distilled water 18 in the liquid storage tank 17. Note that the distilled water discharged at this time is pure water.

Specifically, be provided with defroster 19 in the separating chamber 11, defroster 19 can carry out the defogging to the secondary steam of evaporation production in the separating chamber 11 to get rid of the great liquid drop in the secondary steam, reduce the possibility that the secondary steam carried the particulate matter.

In the embodiment shown in fig. 1, part of the raw liquid introduced into the separation chamber 11 directly enters the separation chamber 11, and part of the raw liquid enters the separation chamber 11 after being heated at the condenser 16, so as to avoid excessive reduction of the heat of the secondary steam, and ensure that the secondary steam can be heated with the primary steam in the subsequent heat exchange process. In other embodiments, the stock solution may be heated and heated in condenser 16 before entering separation chamber 11.

In some embodiments, the cryogenic evaporation system 10 comprises a feed pump 21, and the feed liquid is delivered to the separation chamber 11 by the feed pump 21. By providing the raw liquid transfer pump 21, the raw liquid can be powered so that part of the raw liquid directly enters the separation chamber 11 and part of the raw liquid enters the condenser 16 and then enters the separation chamber 11. Specifically, in the present embodiment, the stock solution feed pump 21 is a horizontal centrifugal pump.

In some embodiments, the cryogenic evaporation system 10 includes a heat exchanger 22, and the heat exchanger 22 is connected to the heater 12, the separation chamber 11, and the air compressor 13. The circulating liquid is evaporated in the separation chamber 11 to generate secondary steam, the secondary steam is finally introduced into the heat exchanger 22, the temperature of primary steam after heat exchange between the heater 12 and the circulating liquid is reduced, the primary steam is finally introduced into the heat exchanger 22, the secondary steam introduced into the heat exchanger 22 exchanges heat with the primary steam, the temperature of the primary steam is increased, and the primary steam can enter the air compressor 13 to be reused. Therefore, the heat carried by the secondary steam can be utilized, and the heat loss of the system is reduced. Meanwhile, the primary steam enters the air compressor 13 again after heat exchange and is utilized, so that the primary steam can be recycled, the cost is reduced, certain heat is carried by the primary steam, and after the primary steam enters the air compressor 13, the air compressor 13 only needs to apply less energy to the primary steam again to meet the requirement of the heater 12, so that the energy consumption of the air compressor 13 is reduced. Therefore, the whole low-temperature evaporation system 10 can stably operate at lower cost by reducing the heat loss and the energy consumption of the system.

In the embodiment shown in fig. 1, the secondary steam generated by evaporation in the separation chamber 11 is introduced into the heat exchanger 22 after the temperature of the condenser 16 has been reduced. In other embodiments, the condenser 16 may be omitted and the secondary steam generated by evaporation in the separation chamber 11 may be passed directly into the heat exchanger 22. In addition, the heat exchanger 22 is a plate heat exchanger, which can make the secondary steam and the primary steam have a larger heat exchange efficiency and reduce heat loss.

Specifically, the cryogenic evaporation system 10 includes a vacuum pump 23 connected to the heat exchanger 22 and a separation tank 24 connected to the vacuum pump 23. The secondary steam after heat exchange at the heat exchanger 22 is discharged to the separation tank 24 by the vacuum pump 23, and is discharged through the separation tank 24. It can be understood that the temperature of the secondary steam of 35-45 ℃ discharged from the condenser 16 is further reduced after the heat exchanger 22 exchanges heat with the primary steam, and the secondary steam is finally discharged at the temperature of 20-30 ℃ under the action of the vacuum pump 23 and the separation tank 24. Specifically, the residual secondary steam which is not easy to condense is extracted by the power provided by the vacuum pump 23, so that a vacuum low-pressure environment can be manufactured for the whole system.

In some embodiments, the cryogenic evaporation system 10 includes a cooling structure 25, and the cooling structure 25 is connected between the heat exchanger 22 and the heater 12 to depressurize and lower the temperature of the primary steam discharged from the heater 12. Specifically, the cooling structure 25 cools primary steam of 35-45 ℃ discharged by the heater 12 to 10-20 ℃, and the temperature of the primary steam is increased to 25-35 ℃ after the primary steam and secondary steam exchange heat after the primary steam and the secondary steam are introduced into the heat exchanger 22. Through the depressurization and the cooling of the cooling structure 25, the primary steam can have smaller pressure after being subjected to heat exchange with the secondary steam, so that the primary steam can be returned to the air compressor 13 again to be recycled.

Specifically, in the embodiment shown in fig. 1, the cooling structure 25 includes a cooling fan 251 and an expansion valve 252, and the heater 12, the cooling fan 251, the expansion valve 252, and the heat exchanger 22 are connected in sequence. The cooling fan 251 primarily cools and reduces the temperature of the primary steam discharged from the heater 12. The expansion valve 252 reduces the pressure and temperature of the primary steam cooled by the cooling fan 251, and converts the high-pressure steam into low-pressure steam. The temperature of the primary steam of 35-45 ℃ discharged by the heater 12 is reduced to 30-40 ℃ after being cooled by the cooling fan 251, but the pressure of the primary steam is still higher, then the primary steam of 10-20 ℃ is obtained after passing through the expansion valve 252, and the primary steam is introduced into the heat exchanger 22 to exchange heat with the secondary steam.

Specifically, in the embodiment shown in fig. 1, the separation chamber 11 has a first inlet 111, a second inlet 112, a liquid outlet 113 and a gas outlet 114. The heater 12 is connected to the second inlet 112 and the liquid outlet 113. The stock solution enters the separation chamber 11 through the first inlet 111, the concentrated solution is discharged to the heater 12 through the solution outlet 113, and after being heated and heated at the heater 12, the concentrated solution enters the separation chamber 11 again through the second inlet 112 for forced circulation evaporation, and finally the formed concentrated solution is discharged to the liquid discharge pump 15 through the solution outlet 113. The secondary steam generated by evaporation in the separation chamber 11 is discharged through the gas outlet 114, and the demister 19 is located at the gas outlet 114. In fig. 1, a is air, B is a stock solution, C is distilled water, D is a concentrated solution, and G is a non-condensable gas. Because whole evaporating system 10 only discharges concentrate, distilled water and noncondensable gas, the higher purity of distilled water can be directly discharged, and noncondensable gas also can not cause the pollution and can directly discharge to the environment, and the concentrate can be handled through the mode of burying to the pollution degree to the environment is less.

In the low temperature evaporation system 10 of this application, the circulation liquid in the separator 11 is circulated through the low temperature steam that utilizes the air compressor machine 13 to produce and is heated, thereby make the circulation liquid maintain in lower temperature, and concentrate step by step in the separator 11, not only can ensure going on smoothly of stoste low temperature evaporation process, but also make whole evaporation system carry out continuous stable work with this state, and need not frequent switching on and shutting down, reduce the energy consumption when reducing the equipment loss. Further, through setting up condenser 16, the secondary steam that makes the evaporation produce in the separator 11 exchanges heat at condenser 16 and stoste to the stoste that makes letting in the separator 11 heaies up, not only can make the heat that the secondary steam carried obtain the utilization, reduces the calorific loss of system, can also reduce the thermal utilization of circulation liquid to primary steam, reduces the energy consumption of air compressor machine 13. Furthermore, by arranging the heat exchanger 22, the primary steam discharged by the heater 12 exchanges heat with the secondary steam generated by evaporation in the separation chamber 11 in the heat exchanger 22 to raise the temperature, and the raised primary steam can enter the air compressor 13 to be reused, so that the heat carried by the secondary steam can be utilized, and the heat loss of the system is reduced. Meanwhile, the primary steam enters the air compressor 13 again after heat exchange and is utilized, so that the primary steam can be recycled, the cost is reduced, certain heat is carried by the primary steam, and after the primary steam enters the air compressor 13, the air compressor 13 only needs to apply less energy to the primary steam again to meet the requirement of the heater 12, so that the energy consumption of the air compressor 13 is reduced. Therefore, the whole low-temperature evaporation system 10 can stably operate at lower cost by reducing the heat loss and the energy consumption of the system.

The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.

The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.

Claims (10)

1. A low-temperature evaporation system is characterized by comprising a separation chamber, a heater and an air compressor; the air compressor is connected with the heater to supply primary steam with the temperature of 45-65 ℃ to the heater; the separation chamber is connected with the heater, the stock solution is evaporated in the separation chamber to form circulating liquid, the circulating liquid exchanges heat with the primary steam in the heater to be heated to 40-60 ℃, then flows into the separation chamber with the internal pressure of 0.03-0.04 MPa to be evaporated, and circularly flows between the separation chamber and the heater to be gradually concentrated.

2. A cryogenic evaporation system according to claim 1, comprising a condenser, wherein the condenser is connected to the separation chamber, the secondary steam generated by evaporation in the separation chamber exchanges heat with the stock solution in the condenser to reduce the temperature, and the heated stock solution enters the separation chamber.

3. A low-temperature evaporation system as claimed in claim 2, wherein the secondary steam generated by evaporation in the separation chamber is cooled to 35-45 ℃ after the heat exchange between the condenser and the stock solution is carried out.

4. A cryogenic evaporation system according to claim 2, comprising a liquid storage tank connected to the condenser, the liquid storage tank being capable of collecting distilled water condensed from the secondary steam in the condenser.

5. The low-temperature evaporation system according to claim 1, wherein the low-temperature evaporation system comprises a heat exchanger, the heat exchanger is connected with the heater, the separation chamber and the air compressor, and primary steam discharged by the heater exchanges heat with secondary steam generated by evaporation in the separation chamber in the heat exchanger; the temperature of the primary steam after heat exchange is increased, and the primary steam can enter the air compressor to be reused.

6. A cryogenic evaporation system according to claim 5, comprising a cooling structure connected between the heat exchanger and the heater to depressurise and desuperheat the primary vapour exiting the heater.

7. A low-temperature evaporation system as claimed in claim 6, wherein the cooling structure cools primary steam at 35-45 ℃ discharged from the heater to 10-20 ℃, and the temperature of the primary steam is raised to 25-35 ℃ after the primary steam and secondary steam exchange heat after the primary steam is introduced into the heat exchanger.

8. A cryogenic evaporation system according to claim 6, wherein the cooling structure comprises a cooling fan and an expansion valve, the heater, the cooling fan, the expansion valve, the heat exchanger being connected in series; the cooling fan carries out primary cooling on the primary steam discharged by the heater; and the expansion valve is used for carrying out pressure reduction and temperature reduction on the primary steam cooled by the cooling fan again.

9. A cryogenic evaporation system according to claim 5, comprising a vacuum pump connected to the heat exchanger and a separation tank connected to the vacuum pump; and discharging the secondary steam subjected to heat exchange at the heat exchanger to the separation tank under the action of the vacuum pump, and discharging the secondary steam through the separation tank.

10. A cryogenic vaporization system according to claim 1 further comprising at least one of the following:

the air compressor is a turbine compressor;

the low-temperature evaporation system further comprises a forced circulation pump, and the forced circulation pump is connected between the heater and the separation chamber so as to make a circulating liquid forcibly circulate between the separation chamber and the heater;

the low-temperature evaporation system comprises a stock solution delivery pump, and stock solution is delivered to the separation chamber under the action of the stock solution delivery pump;

the low-temperature evaporation system comprises a liquid discharge pump connected with the separation chamber, circulating liquid in the separation chamber is concentrated step by step to form concentrated liquid, and the concentrated liquid is forcibly discharged from the separation chamber by the liquid discharge pump.

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