Gas-liquid heat and mass transfer and separation system

Abstract

The invention provides a gas-liquid heat and mass transfer and separation system, and belongs to the field of gas-liquid separation. An air inlet of the supergravity device and / or a liquid inlet of the supergravity device are / is connected with the feeding pipe group; the air outlet pipe is connected with an air outlet of the supergravity device; a liquid inlet of the gas-liquid separator is connected with a liquid outlet of the supergravity device; and the liquid outlet pipe is connected with a liquid outlet of the gas-liquid separator. The invention aims to solve the problems of large occupied space, high construction cost and the like of the gas-liquid heat and mass transfer and separation system in the prior art. The technical effects that the occupied space is effectively saved, and the construction cost is reduced are achieved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of gas-liquid separation, and in particular to a gas-liquid heat mass exchange and separation system. BACKGROUND

[0002] In the industrial production system, the gas-liquid heat mass exchange and separation system is a key equipment for carbon capture, energy heat exchange, and mixture rectification process, and mainly has the following problems: Among them, the energy consumption of the absorbent desorption regeneration link in the chemical absorption method carbon capture system is high and depends on the packed tower or plate tower as the core device, not only the construction cost is high, but also a large area of land is occupied; the volume of the open energy tower with packing for energy heat exchange is large, the area of the installation site is required, and the difficulty of factory layout planning is increased; the large tower body manufacturing and complex supporting facility installation of the rectification tower lead to high construction cost and large tower area.

[0003] In summary, the existing gas-liquid heat mass exchange and separation system mostly has the problems of large occupied space and high construction cost. SUMMARY

[0004] The present application provides a gas-liquid heat mass exchange and separation system to solve the defects of large occupied space and high construction cost in the prior art, and effectively saves the occupied space and reduces the construction cost.

[0005] The present application provides a gas-liquid heat mass exchange and separation system, comprising: a feed pipe group; a supergravity device, the gas inlet of the supergravity device and / or the liquid inlet of the supergravity device is connected with the feed pipe group; a gas outlet pipe, the gas outlet pipe is connected with the gas outlet of the supergravity device; a liquid outlet pipe, the liquid outlet pipe is connected with the liquid outlet of the supergravity device.

[0006] In addition, the gas-liquid heat mass exchange and separation system according to the present application can also have the following additional technical features: In some embodiments of the present application, further comprising: a heat exchange device, the heat exchange device has a plurality of heat exchange devices, at least one heat exchange device is installed between the gas outlet pipe and the supergravity device, and at least one heat exchange device is installed between the liquid outlet pipe and the supergravity device.

[0007] In some embodiments of the present application, the feed pipe group comprises: an inlet and outlet pipe, the inlet and outlet pipe is connected with the liquid inlet of the supergravity device, and at least one heat exchange device is installed between the inlet and outlet pipe and the supergravity device; a gas inlet pipe, the gas inlet pipe is connected with the gas inlet of the supergravity device.

[0008] In some embodiments of the present application, further comprising: A first pipeline, one end of the first pipeline is connected with the supergravity device, and the other end of the first pipeline is connected with the gas outlet pipe; A first compressor, the first compressor is installed on the first pipeline.

[0009] In some embodiments of the present application, further comprising: A second pipeline, one end of the second pipeline is connected with the supergravity device, and the other end of the second pipeline is connected with the gas-liquid separator; A second compressor, the second compressor is installed on the second pipeline.

[0010] In some embodiments of the present application, further comprising: A gas-liquid separator, a liquid inlet of the gas-liquid separator is connected with a liquid outlet of the supergravity device; A third pipeline, one end of the third pipeline is connected with the gas-liquid separator; A pump, the pump is installed on the third pipeline; A fourth pipeline, one end of the fourth pipeline is connected with the gas-liquid separator after passing through the heat exchange device between the gas outlet pipe and the supergravity device, the other end of the fourth pipeline is connected with the liquid outlet pipeline, and the other end of the third pipeline is connected with the middle part of the fourth pipeline.

[0011] In some embodiments of the present application, further comprising: A fifth pipeline, one end of the fifth pipeline is connected with the liquid inlet of the supergravity device, and the other end of the fifth pipeline is connected with the inlet and outlet pipe; A sixth pipeline, one end of the sixth pipeline is connected with the gas outlet of the supergravity device, and the other end of the sixth pipeline is connected with the inlet and outlet pipe.

[0012] In some embodiments of the present application, further comprising: A seventh pipeline, one end of the seventh pipeline is connected with the liquid inlet of the supergravity device, and the second end of the seventh pipeline is connected with the middle part of the sixth pipeline; A liquid inlet pipe, the liquid inlet pipe is connected with the middle part of the seventh pipeline.

[0013] In some embodiments of the present application, further comprising: An eighth pipeline, one end of the eighth pipeline is connected with the mechanical seal bearing inlet and outlet circulating water connection system of the supergravity device; A first heat exchanger, the other end of the eighth pipeline is connected with the first heat exchanger; A working medium circulation pipeline, the working medium circulation pipeline is sequentially arranged on the heat exchange device located on the inlet and outlet pipe, the first heat exchanger, and the heat exchange device located between the liquid outlet pipe and the supergravity device; A ninth pipeline, both ends of the ninth pipeline are connected with the working medium circulation pipeline; The third compressor is installed on the ninth pipeline, one end of the working medium circulation pipeline is connected with one end of the third compressor, and the other end of the working medium circulation pipeline is connected with the other end of the third compressor.

[0014] In some embodiments of the present application, further comprising: The liquid level meter is installed on the gas-liquid separator.

[0015] In summary, the present application has the following beneficial technical effects: the supergravity device can effectively improve the speed of gas-liquid separation, and the supergravity device has small size and small occupation area, so that the gas-liquid heat mass exchange and separation system does not need large towers, thereby effectively saving the occupation area, reducing the construction cost, effectively increasing the gas-liquid separation efficiency, and being applicable to small-scale application scenarios. BRIEF DESCRIPTION OF DRAWINGS

[0016] Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are for purposes of illustration only and are not to be construed as limiting the application. Moreover, in the drawings, like reference numerals designate similar parts throughout the several views, and in which: Figure 1 The structure of the gas-liquid heat mass exchange and separation system according to some embodiments of the present application is schematically shown.

[0017] Reference Signs: 1, first heat exchanger, 2, second heat exchanger, 3, third heat exchanger, 4, fourth heat exchanger, 5, gas-liquid separator, 6, supergravity device, 7, first compressor, 8, second compressor, 9, third compressor, 10, pump, 11, first valve, 12, second valve, 13, third valve, 14, fourth valve, 15, fifth valve, 16, sixth valve, 17, seventh valve, 18, eighth valve, 19, ninth valve, 20, tenth valve, 21, eleventh valve, 22, twelfth valve, 23, thirteenth valve, 24, fourteenth valve, 25, fifteenth valve, 26, sixteenth valve, 27, seventeenth valve, 28, eighteenth valve, 29, first pressure sensor, 30, second pressure sensor, 31, liquid level meter, 32, gas outlet pipe, 33, inlet and outlet pipe, 34, liquid outlet pipe, 35, gas inlet pipe, 36, liquid inlet pipe, 37, first pipeline, 38, second pipeline, 39, third pipeline, 40, fourth pipeline, 41, fifth pipeline, 42, sixth pipeline, 43, seventh pipeline, 44, eighth pipeline, 45, ninth pipeline, 46, working medium circulation pipeline, 47, tenth pipeline, 48, eleventh pipeline, 49, twelfth pipeline, 50, thirteenth pipeline. DETAILED DESCRIPTION

[0018] Example embodiments of the present disclosure will be described below in greater detail with reference to the accompanying drawings. While example embodiments of the present disclosure are shown in the drawings, it is understood that the present disclosure can be implemented in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that the present disclosure will be thoroughly and completely understood, and will fully convey the scope of the present disclosure to those skilled in the art.

[0019] It is to be understood that the terms used herein are merely for the purpose of describing particular example embodiments and are by no means intended to be limiting. As used herein, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. The terms "comprises," "comprising," "includes," "including," and the like are inclusive and therefore specify the presence of stated features, steps, operations, elements, and / or components, but do not preclude the presence or addition of one or more other features, steps, operations, elements, components, and / or groups thereof. The method steps, processes, and operations described herein are not to be construed as necessarily requiring their performance in the particular order in which they are described, unless specifically identified as an order dependent step. It is also to be understood that additional or alternative steps can be employed.

[0020] Although the terms first, second, third, and the like can be used herein to describe various elements, components, regions, layers and / or sections, these elements, components, regions, layers and / or sections should not be limited by these terms. These terms can be only used to distinguish one element, component, region, layer or section from another region, layer or section. Terms such as "first," "second," and other numerical terms when used herein do not imply a sequence or order unless clearly indicated by the context. Thus, a first element, component, region, layer or section discussed below could be termed a second element, component, region, layer or section without departing from the teachings of the example embodiments.

[0021] Spatially relative terms, such as "inner," "outer," "inwardly," "outwardly," "lower," "bottom," "top," "upper," and the like, can be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. Spatially relative terms can be intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if the device in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" or "over" the other elements or features. Thus, the example term "below" can encompass both an orientation of above and below. The device can be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.

[0022] In industrial production, gas-liquid heat and mass exchange and separation systems are important equipment for realizing processes such as carbon capture, energy heat exchange, and mixture distillation. However, current traditional gas-liquid heat and mass exchange and separation systems generally suffer from the core problems of large footprint and high construction costs, as well as low operating efficiency and poor economic performance. Specifically, existing chemical absorption carbon capture systems have the following drawbacks: high energy consumption for absorbent desorption and regeneration; the tower requires a considerable amount of corrosion-resistant material, resulting in high construction costs and a large footprint; regardless of whether it is a packed tower or a plate tower, the mass transfer efficiency is not high enough, requiring a large tower volume and solution circulation volume, which leads to high equipment and operating costs; overall, the economic viability for small-scale applications is low.

[0023] Existing packed-type open energy towers use sprayed antifreeze to exchange heat and mass with air in a countercurrent manner, absorbing the sensible heat of the air and the latent heat of water vapor in the air, while transferring the heat to the heat pump to achieve heating or heat supply. However, they are also large in size and there is a certain risk of sprayed liquid drift.

[0024] Existing distillation columns also have drawbacks such as high construction costs, large footprint, insufficient mass transfer efficiency, and high operating costs.

[0025] like Figure 1 As shown, according to an embodiment of the first aspect of the present invention, a gas-liquid heat and mass exchange and separation system is proposed, including a hypergravity device 6, a gas-liquid separator 5, a feed pipe assembly, an air outlet pipe 32, and a liquid outlet pipe 34. The air inlet and / or the liquid inlet of the hypergravity device 6 are connected to the feed pipe assembly, the air outlet pipe 32 is connected to the air outlet of the hypergravity device 6, the liquid inlet of the gas-liquid separator 5 is connected to the liquid outlet of the hypergravity device 6, and the liquid outlet pipe 34 is connected to the liquid outlet of the gas-liquid separator 5.

[0026] In the above embodiments, it should be noted that a first pressure sensor 29 is also included, which is installed on the hypergravity device 6; the hypergravity device 6 can be an existing filler-type hypergravity device 6 or a rotating plate-type hypergravity device 6.

[0027] The supergravity device 6 is a highly efficient gas-liquid mass transfer device that can be used for the separation, purification, and recovery of organic solvents. It consists of one or more high-speed rotating rotors, through which gas and liquid are transferred in a counter-current spray manner. It has many advantages such as high efficiency, low energy consumption, high mass transfer rate, short gas-liquid residence time, small liquid holdup, strong anti-clogging ability, safety and reliability, easy operation, easy cleaning, large processing capacity, and small footprint.

[0028] The technical effects achieved by the above embodiment are that: the supergravity device 6 can effectively improve the speed of gas-liquid separation, and the supergravity device 6 has small size and small footprint, and the gas-liquid separation device 5 has compact structure, so that the whole gas-liquid heat mass exchange and separation system does not need large tower, effectively saves the floor space, reduces the construction cost, effectively increases the gas-liquid separation efficiency, and can be applied to small-scale application scenarios.

[0029] Optionally, as shown in Figure 1 The heat exchange device is provided between the gas outlet pipe 32 and the supergravity device 6, and the heat exchange device is provided between the liquid outlet pipe 34 and the supergravity device 6.

[0030] The beneficial effects of the above optional embodiment are that: the heat energy can be effectively recycled for gas-liquid separation by the heat exchange device, thereby increasing the utilization of heat energy and reducing energy consumption.

[0031] Optionally, as shown in Figure 1 The feed pipe group includes the inlet and outlet pipe 33 and the gas inlet pipe 35, the inlet and outlet pipe 33 is connected with the liquid inlet of the supergravity device 6, and the gas inlet pipe 35 is connected with the gas inlet of the supergravity device 6; at least one heat exchange device is installed between the inlet and outlet pipe 33 and the supergravity device 6.

[0032] In the above optional embodiment, it should be noted that the heat exchange device includes the second heat exchanger 2, the third heat exchanger 3 and the fourth heat exchanger 4, the second heat exchanger 2 is installed between the gas outlet pipe 32 and the supergravity device 6; the third heat exchanger 3 is installed between the inlet and outlet pipe 33 and the supergravity device 6; and the fourth heat exchanger 4 is installed between the liquid outlet pipe 34 and the supergravity device 6.

[0033] The beneficial effects of the above optional embodiment are that: the reliable feeding of gas or liquid and the reliable discharge of gas or liquefied gas after passing through the heat exchange device are realized by the gas inlet pipe 35 and the inlet and outlet pipe 33.

[0034] Optionally, as shown in Figure 1 The first compressor 7 and the first pipeline 37 are further included, one end of the first pipeline 37 is connected with the supergravity device 6, the other end of the first pipeline 37 is connected with the gas outlet pipe 32, and the first compressor 7 is installed on the first pipeline 37.

[0035] In the above optional embodiment, it should be noted that the second pressure sensor 30 is further included, the second pressure sensor 30 is installed on the first pipeline 37; the valve is installed on the first pipeline 37, and the valve on the first pipeline 37 is located between the first compressor 7 and the supergravity device 6; and the first compressor 7 can be a Roots compressor, a screw compressor or a centrifugal compressor.

[0036] Optionally, as shown in Figure 1 The second compressor 8 is installed on the second pipeline 38.

[0037] In the above-mentioned optional embodiment, it should be noted that the second compressor 8 can be a Roots compressor, a screw compressor or a centrifugal compressor.

[0038] The above-mentioned optional embodiment has the beneficial effect that the first compressor 7 and the second compressor 8 can consume a small amount of electric energy, and the technology of increasing the temperature and pressure of a large amount of low-temperature steam to high-temperature steam that can be used, and recovering the waste steam that is originally discharged and using it for heating again, can greatly save energy consumption.

[0039] Optionally, as shown in Figure 1 The fourth pipeline 40 is connected to the gas-liquid separator 5 through the heat exchange device between the gas outlet pipe 32 and the supergravity device 6, and the other end of the fourth pipeline 40 is connected to the liquid outlet pipe 34. The pump 10 is installed on the third pipeline 39.

[0040] In the above-mentioned optional embodiment, it should be noted that the fourth pipeline 40 is provided with a valve, and the valve on the fourth pipeline 40 is located between the second heat exchanger 2 and the connection point of the third pipeline 39 and the fourth pipeline 40; the pump 10 is a heat pump.

[0041] The above-mentioned optional embodiment has the beneficial effect that the heat cycle of the heat exchange medium of the system can be effectively realized by the pump 10, thereby increasing the utilization efficiency of heat energy and indirectly reducing energy consumption.

[0042] Optionally, as shown in Figure 1 The fifth pipeline 41 is connected to the liquid inlet of the supergravity device 6, and the other end of the fifth pipeline 41 is connected to the inlet and outlet pipe 33. The sixth pipeline 42 is connected to the gas outlet of the supergravity device 6, and the other end of the sixth pipeline 42 is connected to the inlet and outlet pipe 33.

[0043] In the above-mentioned optional embodiment, it should be noted that the sixth pipeline 42 is connected to the inlet and outlet pipe 33 through the third heat exchanger 3, and the valves are installed on the fifth pipeline 41 and the sixth pipeline 42.

[0044] The beneficial effect of the above-mentioned optional embodiment is that the liquid rectification into and discharge after rectification of the rectification process can be effectively realized by the fifth pipeline 41 and the sixth pipeline 42, and the gas-liquid separation effect is increased.

[0045] Optionally, as shown in Figure 1 the seventh pipeline 43, one end of the seventh pipeline 43 is connected with the liquid inlet of the supergravity device 6, the second end of the seventh pipeline 43 is connected with the middle part of the sixth pipeline 42, and the liquid inlet pipe 36 is connected with the middle part of the seventh pipeline 43.

[0046] In the above-mentioned optional embodiment, it should be noted that the liquid inlet pipe 36 is provided with a valve, the seventh pipeline 43 is provided with a valve, the valve on the seventh pipeline 43 is located between the connection point of the liquid inlet pipe 36 and the seventh pipeline 43 and the connection point of the seventh pipeline 43 and the sixth pipeline 42, and the valve on the sixth pipeline 42 is located between the gas outlet of the supergravity device 6 and the connection point of the sixth pipeline 42 and the seventh pipeline 43.

[0047] Optionally, as shown in Figure 1 the first heat exchanger 1, the eighth pipeline 44, the ninth pipeline 45, the third compressor 9 and the working medium circulation pipeline 46, one end of the eighth pipeline 44 is connected with the machine seal bearing in-out circulating water connection system of the supergravity device 6, the other end of the eighth pipeline 44 is connected with the first heat exchanger 1, the working medium circulation pipeline 46 is sequentially arranged on the heat exchange device on the in-out pipe 33, the first heat exchanger 1 and the heat exchange device between the liquid outlet pipe 34 and the supergravity device 6, the two ends of the ninth pipeline 45 are respectively connected with the working medium circulation pipeline 46, the third compressor 9 is installed on the ninth pipeline 45, the first end of the working medium circulation pipeline 46 is connected with one end of the third compressor 9, and the second end of the working medium circulation pipeline 46 is connected with the other end of the third compressor 9.

[0048] In the optional embodiment, it is to be noted that the tenth pipeline 47, the eleventh pipeline 48, the twelfth pipeline 49 and the thirteenth pipeline 50 are further included, one end of the tenth pipeline 47 is connected with the liquid outlet of the supergravity device 6, the other end of the tenth pipeline 47 is connected with the middle part of the thirteenth pipeline 50, one end of the thirteenth pipeline 50 is connected with the middle part of the fourth pipeline 40, the other end of the thirteenth pipeline 50 is connected with the liquid outlet pipe 34 through the fourth heat exchanger 4, and a valve is installed on the thirteenth pipeline 50; a valve is arranged between the connection point of the thirteenth pipeline 50 and the fourth pipeline 40 and the connection point of the liquid outlet pipe 34 and the fourth pipeline 40, and the valve is installed on the fourth pipeline 40; both ends of the eleventh pipeline 48 are connected with the third pipeline 39, one end of the eleventh pipeline 48 is located between the pump 10 and the gas-liquid separator 5, and the other end of the eleventh pipeline 48 is located between the pump 10 and the fourth pipeline 40, and a valve is installed on the eleventh pipeline 48; one end of the twelfth pipeline 49 is connected with the gas-liquid separator 5, and the other end of the twelfth pipeline 49 is connected with the supergravity device 6.

[0049] The working medium circulation pipeline 46 is sequentially arranged on the third heat exchanger 3, the first heat exchanger 1 and the fourth heat exchanger 4.

[0050] The third compressor 9 can be a Roots compressor, a screw compressor or a centrifugal compressor.

[0051] The specific selection of the heat pump circulation working medium in the working medium circulation pipeline 46 is as follows: when the required condensation temperature is 40-60℃, R410A working medium is preferred; when the condensation temperature is 50-80℃, R134A working medium is preferred; when the condensation temperature is 70-100℃, R515B working medium is preferred; when the condensation temperature is 90-120℃, R245FA working medium is preferred; and when the condensation temperature is 110-150℃, R718 working medium is preferred.

[0052] The optional embodiment has the beneficial effect that the energy consumption of the coupled compression enthalpy increase can be effectively reduced by the combination of the first compressor 7, the second compressor 8, the third compressor 9 and the pump 10.

[0053] Optionally, as shown in Figure 1 The liquid level meter 31 is installed on the gas-liquid separator 5.

[0054] The optional embodiment has the beneficial effect that the liquid level in the gas-liquid separator 5 can be effectively monitored by the liquid level meter 31, thereby ensuring the reliability of the work.

[0055] Specifically, this gas-liquid heat and mass exchange and separation system also includes a first valve 11, a second valve 12, a third valve 13, a fourth valve 14, a fifth valve 15, a sixth valve 16, a seventh valve 17, an eighth valve 18, a ninth valve 19, a tenth valve 20, an eleventh valve 21, a twelfth valve 22, a thirteenth valve 23, a fourteenth valve 24, a fifteenth valve 25, a sixteenth valve 26, a seventeenth valve 27, and an eighteenth valve 28; the first valve 11 is installed on the air inlet pipe 35, the second valve 12 is installed on the liquid inlet pipe 36, and the third valve 13 is installed on the fourth pipeline 40 and is located at... The fourth valve 14 is installed on the sixth pipe 42 and located between the outlet of the supergravity device 6 and the seventh pipe 43; the fifth valve 15 is installed on the sixth pipe 42 and located between the inlet pipe 36 and the sixth pipe 42; the sixth valve 16 is installed on the tenth pipe 47; the seventh valve 17 is installed on the working fluid circulation pipe 46 and located between the first heat exchanger 1 and the fourth heat exchanger 4; the eighth valve 18 is installed on the thirteenth pipe 50 and located between the tenth pipe 47 and the fourth pipe 40; the ninth valve 19 is installed on the fourth pipe 47. The tenth valve 20 is installed on the eleventh pipe 48 and between the thirteenth pipe 50 and the outlet pipe 34; the eleventh valve 21 is installed on the first pipe 37 and between the outlet of the first compressor 7 and the outlet of the hypergravity device 6; the twelfth valve 22 is installed on the outlet pipe 34; the thirteenth valve 23 is installed on the working fluid circulation pipe 46 and between the connection point of the ninth pipe 45 and the first end of the working fluid circulation pipe 46 and the connection point of the second end of the ninth pipe 45 and the working fluid circulation pipe 46; the fourteenth valve 24 is installed on the ninth pipe 45 and between the first end of the ninth pipe 45 and the working fluid circulation pipe 46. The connection point of the circulation pipeline 46 is between the first end of the working fluid circulation pipeline 46; the fifteenth valve 25 is installed on the working fluid circulation pipeline 46 and is located between the second end of the working fluid circulation pipeline 46 and the connection point between the second end of the ninth pipeline 45 and the working fluid circulation pipeline 46; the sixteenth valve 26 is installed on the working fluid circulation pipeline 46 and is located between the second end of the working fluid circulation pipeline 46 and the connection point between the first end of the ninth pipeline 45 and the working fluid circulation pipeline 46; the seventeenth valve 27 is installed on the working fluid circulation pipeline 46 and is located between the first heat exchanger 1 and the third heat exchanger 3; the eighteenth valve 28 is installed on the fifth pipeline 41.

[0056] The working principle of this gas-liquid heat and mass exchange and separation system is as follows: The first type of distillation operation procedure: Close the fifth valve 15. The feed liquid enters the centrifugal device 6 through the inlet pipe 36 and the open second valve 12. After distillation, it flows by gravity from the bottom outlet of the centrifugal device 6 to the gas-liquid separator 5. Close the eleventh valve 21. The overhead gas from the distillation column of the centrifugal device 6 enters the third heat exchanger 3 through the open fourth valve 14, releases heat, condenses, and is discharged from the inlet / outlet pipe 33. Adjust the opening of the eighteenth valve 28 to control the amount of overhead gas condensate returning to the centrifugal device 6. Open... Fourteenth valve 24 and fifteenth valve 25 are closed, thirteenth valve 23 and sixteenth valve 26 are closed, the working fluid absorbs heat and evaporates in the third heat exchanger 3, and then enters the third compressor 9 through fourteenth valve 24. After increasing enthalpy, temperature and pressure, it enters the fourth heat exchanger 4 through fifteenth valve 25 for condensation. After condensation, the working fluid passes through the seventh valve 17 for throttling and cooling and pressure reduction, and enters the first heat exchanger 1 to absorb heat from the circulating water of the mechanical seal bearing of the gravity device 6, and then enters the third heat exchanger 3 through the seventeenth valve 27. Open valves 16, 19, and 22, start pump 10, and close valves 13, 18, and 20. Adjust valve 22 to control the amount of bottom liquid discharged from pipe 34, with the liquid level of gas-liquid separator 5 as the target. Pump 10 pumps the bottom liquid through valve 19 into the fourth heat exchanger 4 for heat absorption and evaporation. The gas-liquid mixed bottom liquid returns to the bottom of the supergravity device 6 through valve 16. The vapor rises and contacts the liquid to complete the distillation.

[0057] The second type of distillation column operation procedure: Close the fifth valve 15. The feed liquid enters the centrifugal device 6 through the inlet pipe 36 and the open second valve 12. After distillation, it flows by gravity from the bottom outlet of the centrifugal device 6 to the gas-liquid separator 5. Close the fourth valve 14. The top gas of the distillation column in the centrifugal device 6 enters the first compressor 7 through the open eleventh valve 21 to increase enthalpy. The frequency of the first compressor 7 is adjusted according to the top pressure of the centrifugal device 6. After heating and pressurization, it enters the second heat exchanger 2 to release heat and condense before being discharged from the outlet pipe 32. Open the third valve 13, the ninth valve 19, and... The twelfth valve 22 is used to start pump 10 and close the first valve 11, the sixth valve 16, the eighth valve 18 and the tenth valve 20. The amount of liquid discharged from the bottom of the column through the outlet pipe 34 is controlled by adjusting the twelfth valve 22 according to the liquid level of the gas-liquid separator 5. Pump 10 pumps the bottom liquid through the third valve 13 into the second heat exchanger 2 for heat absorption and evaporation, and then returns to the gas-liquid separator 5. The second compressor 8 is started to extract flash steam and increase enthalpy. The frequency of the second compressor 8 is adjusted according to the pressure at the top of the gas-liquid separator 5. After the temperature and pressure are increased, the steam enters the supergravity device 6 and rises to contact the feed liquid to complete the distillation.

[0058] Operational flow of the chemical absorption carbon capture tower: Flue gas enters the gas-liquid separator 5 through the inlet pipe 35 and the first valve 11. The second compressor 8 is turned on to discharge the flue gas into the gravity device 6. The eleventh valve 21 is opened, the fourth valve 14 is closed, and the first compressor 7 is turned on to discharge the top gas from the tower through the outlet pipe 32. The second valve 12 and the eighteenth valve 28 are closed, and the fifth valve 15 is opened. The lean liquid enters the third heat exchanger 3 through the inlet and outlet pipes 33, releases heat and cools down, and then enters the gravity device 6 through the fifth valve 15. The rich liquid flows from the bottom outlet of the gravity device 6 to the gas-liquid separator 5 by gravity. The eighth valve 18 and the twelfth valve 22 are opened, and the third valve 13, the sixth valve 16, and the ninth valve are closed. Gate 19 and tenth valve 20 are used to start pump 10, which pumps the rich liquid into the fourth heat exchanger 4 to absorb heat and increase its temperature. After that, it is discharged from the outlet pipe 34 through the twelfth valve 22. Then, the seventh valve 17, fourteenth valve 24, fifteenth valve 25 and seventeenth valve 27 are opened, and the thirteenth valve 23 and sixteenth valve 26 are closed. The heat pump working fluid absorbs heat and evaporates through the third heat exchanger 3. After passing through the fourteenth valve 24, it enters the third compressor 9. After being heated and pressurized, it is discharged from the third compressor 9. After passing through the fifteenth valve 25, it enters the fourth heat exchanger 4 to release heat and condense. After passing through the seventh valve 17 to reduce its temperature and pressure, it enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6. Then, it enters the third heat exchanger 3 through the seventeenth valve 27 to complete the working fluid cycle.

[0059] The first type of chemical absorption carbon capture and desorption tower operation procedure is as follows: Close the second valve 12, the fourth valve 14, and the eighteenth valve 28; open the fifth valve 15. The rich liquid enters the third heat exchanger 3 from the inlet / outlet pipe 33, absorbs heat and heats up, then passes through the fifth valve 15 and enters the hypergravity device 6. Close the first valve 11, the sixth valve 16, and the tenth valve 20; open the third valve 13, the eighth valve 18, and the twelfth valve 22. The lean liquid flows from the bottom outlet of the hypergravity device 6 to the gas-liquid separator 5 by gravity. Start the pump 10 to pump the lean liquid into the second heat exchanger 2 for heat absorption and heat increase, then return it to the gas-liquid separator 5. Start the second compressor 8; adjust the frequency of the second compressor 8 according to the pressure at the top of the gas-liquid separator 5. The flash vapor passes through the second compressor 8 for heating and pressurization before being discharged into the hypergravity device 6 for desorption. Open the eleventh valve 21; start the first compressor 7; adjust the frequency of the first compressor 7 according to the pressure at the top of the hypergravity device 6. The vapor discharged from the top of the hypergravity device 6... The regenerated gas enters the first compressor 7 through the eleventh valve 21, and after being heated and pressurized, it is discharged into the second heat exchanger 2 to release heat and condense some of the water, and then discharged from the outlet pipe 32. Another path of lean liquid from the pump 10 outlet enters the fourth heat exchanger 4 through the eighth valve 18 to release heat, and then exits through the twelfth valve 22 to exit through the liquid outlet pipe 34. The amount of lean liquid discharged through the liquid outlet pipe 34 is controlled by adjusting the twelfth valve 22 according to the liquid level of the gas-liquid separator 5. The seventh valve 17, the thirteenth valve 23, the sixteenth valve 26 and the seventeenth valve 27 are opened, and the fourteenth valve 24 and the fifteenth valve 25 are closed. The heat pump working fluid absorbs heat and evaporates through the fourth heat exchanger 4, and then enters the third compressor 9 through the thirteenth valve 23. After being heated and pressurized, it is discharged from the third compressor 9, enters the third heat exchanger 3 through the sixteenth valve 26 to release heat and condense, and then enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6 through the seventeenth valve 27 to enter the fourth heat exchanger 4 to complete the working fluid cycle.

[0060] The second type of chemical absorption carbon capture and desorption tower operation procedure is as follows: Close valves 15 (5th), 21 (11th), and 28 (18th); open valves 12 (2nd) and 14 (4th). Rich liquid enters the supergravity device 6 through inlet pipe 36 and valve 12. Regeneration gas from the top of supergravity device 6 enters the third heat exchanger 3 through valve 14, releasing heat; some water is condensed and discharged through inlet / outlet pipes 33. Close valves 13 (3rd) and 18 (8th); open valves 16 (6th), 19 (9th), 20 (10th), and 22 (12th). Lean liquid enters gas-liquid separator 5, passes through valves 20 (10th) and 19 (9th) into the fourth heat exchanger 4 for heat absorption and evaporation, and returns to the bottom of supergravity device 6 through valve 16. The steam rises and undergoes desorption. The lean liquid continues to be replenished to the gas-liquid separator 5 and then to the fourth heat exchanger 4 through the tenth valve 20. The amount of lean liquid discharged from the outlet pipe 34 is controlled by the twelfth valve 22 according to the liquid level of the gas-liquid separator 5. The seventh valve 17, the fourteenth valve 24, the fifteenth valve 25 and the seventeenth valve 27 are opened, and the thirteenth valve 23 and the sixteenth valve 26 are closed. The heat pump working fluid absorbs heat and evaporates through the third heat exchanger 3 and enters the third compressor 9 through the fourteenth valve 24. After being heated and pressurized, it is discharged from the third compressor 9 and enters the fourth heat exchanger 4 through the fifteenth valve 25 to release heat and condense. After being throttled and cooled and depressurized through the seventh valve 17, it enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6, and then enters the third heat exchanger 3 through the seventeenth valve 27 to complete the working fluid cycle.

[0061] Energy Tower Operation Procedure: Open valves 11, 19, 21, 22, and 28; close valves 12, 13, 14, 15, 16, 18, and 20; start compressors 7 and 8; air is drawn into compressor 8 from inlet pipe 35 through valve 11 and gas-liquid separator 5, and then discharged into inlet of hypergravity device 6 for mass transfer. After heat and mass transfer, the air is discharged from the top of the hypergravity device 6, passes through the eleventh valve 21 and the first compressor 7, and is discharged through the outlet pipe 32. The spray liquid enters the hypergravity device 6 from the inlet pipe 33 through the eighteenth valve 28 for mass and heat transfer. Then the spray liquid enters the gas-liquid separator 5. The pump 10 is turned on to pump the heat-exchanged spray liquid out through the ninth valve 19 and the twelfth valve 22 and is discharged through the outlet pipe 34. The amount of spray liquid discharged through the outlet pipe 34 is controlled by adjusting the twelfth valve 22 according to the liquid level of the gas-liquid separator 5.

[0062] The specific separation case of this separation system is as follows: The first type of distillation function takes ethanol distillation as an example: With the fifth valve 15 closed, 45°C crude ethanol enters the centrifugal device 6 through the inlet pipe 36 and the open second valve 12. After distillation, the dilute alcohol wastewater flows by gravity from the bottom outlet of the centrifugal device 6 to the gas-liquid separator 5. With the eleventh valve 21 closed, 78°C high-concentration ethanol gas from the top of the distillation column in the centrifugal device 6 enters the third heat exchanger 3 through the open fourth valve 14, releasing heat and condensing. The finished ethanol is then discharged from the inlet and outlet pipes 33. Adjust the opening of valve 28 to control the reflux ratio to 3.5; open valves 24 and 25, and close valves 23 and 26. The 60°C working fluid absorbs heat and evaporates in the third heat exchanger 3, then enters the third compressor 9 through valve 24. The compressor is a multi-stage compressor; after increasing enthalpy, temperature, and pressure to 107°C, it enters the fourth heat exchanger 4 through valve 25 for condensation. After condensation, the working fluid is throttled and cooled to 60°C through valve 17, then enters the first heat exchanger 1 to absorb heat from the circulating water of the mechanical seal bearing in the gravity device 6 for evaporation. A small portion then enters the third heat exchanger 3 through the opened seventeenth valve 27; the sixth valve 16, the ninth valve 19, and the twelfth valve 22 are opened, the pump 10 is started, and the third valve 13, the eighth valve 18, and the tenth valve 20 are closed. The twelfth valve 22 is adjusted to control the amount of wastewater discharged from the outlet pipe 34 based on the liquid level of the gas-liquid separator 5. The pump 10 pumps the 102℃ wastewater through the ninth valve 19 into the fourth heat exchanger 4 for heat absorption and evaporation. The gas-liquid mixture at the bottom of the tower returns to the bottom of the supergravity device 6 through the sixth valve 16. The steam rises and contacts the feed liquid to complete the distillation.

[0063] The second type of distillation column function takes ethanol distillation as an example: with the fifth valve 15 closed, crude ethanol at 40℃ enters the high gravity device 6 through the inlet pipe 36 and the open second valve 12. After distillation, the dilute alcohol wastewater flows by gravity from the bottom outlet of the hypergravity device 6 to the gas-liquid separator 5. The fourth valve 14 is closed, and the high-concentration ethanol gas at 78°C at the top of the distillation column of the hypergravity device 6 enters the first compressor 7 through the opened eleventh valve 21 to increase enthalpy. The frequency of the first compressor 7 is adjusted according to the pressure at the top of the hypergravity device 6. After heating and pressurizing to 97°C, it enters the second heat exchanger 2 to release heat and condense before being discharged from the outlet pipe 32. The third valve 13, the ninth valve 19, and the twelfth valve 22 are opened, pump 10 is started, and the first valve is closed. Valve 11, valve 16, valve 18, and valve 20, along with valve 22, control the amount of wastewater discharged from the outlet pipe 34 by adjusting valve 22 according to the liquid level of gas-liquid separator 5. Pump 10 pumps out 92°C wastewater through valve 13 into the second heat exchanger 2 for heat absorption and evaporation, then returns to gas-liquid separator 5. The second compressor 8 is turned on to extract flash steam and increase enthalpy. The frequency of the second compressor 8 is adjusted according to the pressure at the top of gas-liquid separator 5. After the temperature and pressure are increased to 102°C, the steam enters the supergravity device 6, rises, and contacts the liquid to complete the distillation.

[0064] Taking a 500-ton / year carbon capture system as an example, the function of a chemical absorption carbon capture tower is as follows: 400 m³ / h, 40℃ flue gas enters the gas-liquid separator 5 through the inlet pipe 35 via the opened first valve 11; the second compressor 8 is activated to discharge the flue gas into the gravity device 6; the eleventh valve 21 is opened, the fourth valve 14 is closed, and the first compressor 7 is activated to discharge the top gas from the tower through the outlet pipe 32; the second valve 12 and the eighteenth valve 28 are closed, and the fifth valve 15 is opened. 2 m³ / h of lean liquor enters the third heat exchanger 3 through inlet / outlet pipe 33, releasing heat and cooling to 40°C. It then passes through the fifth valve 15 and enters the centrifugal device 6. Rich liquor flows from the bottom outlet of the centrifugal device 6 to the gas-liquid separator 5 by gravity. The eighth valve 18 and the twelfth valve 22 are opened, while the third valve 13, sixth valve 16, ninth valve 19, and tenth valve 20 are closed. Pump 10 is started, pumping 2 m³ / h of rich liquor into the fourth heat exchanger 4 to absorb heat and increase its temperature. It then exits through the twelfth valve 22 and exits through the outlet pipe 34. The seventh valve 17 is then opened. Fourteenth valve 24, fifteenth valve 25 and seventeenth valve 27, and thirteenth valve 23 and sixteenth valve 26 are closed. The heat pump working fluid absorbs heat and evaporates through the third heat exchanger 3, then enters the third compressor 9 through the fourteenth valve 24. After being heated and pressurized, it is discharged from the third compressor 9, enters the fourth heat exchanger 4 through the fifteenth valve 25 to release heat and condense. After being throttled and cooled and depressurized through the seventh valve 17, it enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6, and then enters the third heat exchanger 3 through the seventeenth valve 27 to complete the working fluid cycle.

[0065] The first type of chemical absorption carbon capture and desorption tower function takes a 500-ton / year carbon capture system as an example: The second valve 12, the fourth valve 14, and the eighteenth valve 28 are closed, and the fifth valve 15 is opened. A 2 m³ / h rich liquid enters the third heat exchanger 3 from the inlet / outlet pipe 33, absorbs heat and increases temperature, then passes through the fifth valve 15 and enters the supergravity device 6. The first valve 11, the sixth valve 16, and the tenth valve 20 are closed, and the third valve 13, the eighth valve 18, and the twelfth valve 22 are opened. The lean liquid flows from the bottom outlet of the supergravity device 6 to the gas-liquid separator 5 by gravity. Pump 10 is started, pumping the lean liquid at a rate of 15 m³ / h into the second heat exchanger 2 for heat absorption and increases temperature, then returning it to the gas-liquid separator 5. The second compressor 8 is started, and its frequency is adjusted according to the pressure at the top of the gas-liquid separator 5. The flashed steam is heated and pressurized to 110°C by the second compressor 8 before being discharged into the supergravity device 6 for desorption. Open the eleventh valve 21 and start the first compressor 7. Adjust the frequency of the first compressor 7 according to the pressure at the top of the hypergravity device 6. The regeneration gas discharged from the top of the hypergravity device 6 enters the first compressor 7 through the eleventh valve 21. After being heated and pressurized, it is discharged into the second heat exchanger 2 to release heat and condense the water. Then it is discharged from the gas outlet pipe 32. Another path of lean liquid from the outlet of pump 10 enters the fourth heat exchanger 4 through the eighth valve 18 to release heat and then passes through the twelfth valve 22 to discharge into the liquid outlet pipe 34. Adjust the twelfth valve 22 according to the liquid level of the gas-liquid separator 5 to control the lean liquid to be discharged into the liquid outlet pipe 34 at a rate of 2 m³ / h. Open valves 17, 23, 26, and 27, and close valves 24 and 25. The heat pump working fluid absorbs heat and evaporates through the fourth heat exchanger 4, then enters the third compressor 9 through valve 23. After being heated and pressurized, it is discharged from the third compressor 9, enters the third heat exchanger 3 through valve 26 to release heat and condense, and then enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6 through valve 27. Finally, it enters the fourth heat exchanger 4 through valve 17 to complete the working fluid cycle.

[0066] The second type of chemical absorption carbon capture desorption tower function, taking a 500-ton / year carbon capture system as an example: The fifth valve 15, eleventh valve 21, and eighteenth valve 28 are closed. The second valve 12 and fourth valve 14 are opened. A 2 m³ / h rich liquid enters the supergravity device 6 through the inlet pipe 36 and the second valve 12. The regeneration gas at the top of the supergravity device 6 enters the third heat exchanger 3 through the fourth valve 14, releasing heat through water condensation, and then exits through the inlet and outlet pipes 33. The third valve 13 and eighth valve 18 are closed. The sixth valve 16, ninth valve 19, tenth valve 20, and twelfth valve 22 are opened. A 110℃ lean liquid enters the gas-liquid separator 5, passes through the tenth valve 20 and the ninth valve 19, enters the fourth heat exchanger 4 for heat absorption and evaporation, and returns to the bottom of the supergravity device 6 through the sixth valve 16. The steam rises to ℃ for desorption, and the lean liquid continues to be replenished to the gas-liquid separator 5, and then to the fourth heat exchanger 4 through the tenth valve 20. According to the liquid level of the gas-liquid separator 5, the twelfth valve 22 controls the lean liquid to be discharged from the outlet pipe 34 at a rate of 2m³ / h. The seventh valve 17, the fourteenth valve 24, the fifteenth valve 25 and the seventeenth valve 27 are opened, and the thirteenth valve 23 and the sixteenth valve 26 are closed. The heat pump working fluid absorbs heat and evaporates through the third heat exchanger 3, and then enters the third compressor 9 through the fourteenth valve 24. After being heated and pressurized, it is discharged from the third compressor 9 and enters the fourth heat exchanger 4 through the fifteenth valve 25 to release heat and condense. After being throttled and cooled and depressurized through the seventh valve 17, it enters the first heat exchanger 1 to absorb heat from the oil temperature of the hypergravity device 6, and then enters the third heat exchanger 3 through the seventeenth valve 27 to complete the working fluid cycle.

[0067] Taking a 400t / h circulation tower as an example: The following steps are implemented: First valve 11, Ninth valve 19, Eleventh valve 21, Twelfth valve 22, and Eighteenth valve 28 are opened; Second valve 12, Third valve 13, Fourth valve 14, Fifth valve 15, Sixth valve 16, Eighth valve 18, and Tenth valve 20 are closed; First compressor 7 and Second compressor 8 are started; 400,000 m³ / h of air is drawn into Second compressor 8 through inlet pipe 35, passing through First valve 11 and gas-liquid separator 5, and then discharged into the inlet of the hypergravity device 6. Mass and heat transfer occurs, and the air after mass and heat transfer is discharged from the top of the hypergravity device 6, passing through the eleventh valve 21 and the first compressor 7, and then discharged through the outlet pipe 32. The 400t / h spray liquid enters the hypergravity device 6 from the inlet / outlet pipe 33 through the eighteenth valve 28 for mass and heat transfer. After that, the spray liquid enters the gas-liquid separator 5. The pump 10 is turned on to pump the heat-exchanged spray liquid out through the ninth valve 19 and the twelfth valve 22 and discharged through the outlet pipe 34. The spray liquid is discharged through the outlet pipe 34 at a rate of 400t / h according to the liquid level of the gas-liquid separator 5 and the twelfth valve 22.

[0068] In summary, this system has the following advantages: First, it boasts high efficiency, low energy consumption, high mass transfer rate, short gas-liquid residence time, small liquid holdup, large processing capacity, and low operating costs. Second, it requires fewer materials to manufacture, resulting in lower construction costs and a smaller footprint. Third, it exhibits strong anti-clogging capabilities, is safe and reliable, easy to operate and clean, and requires relatively easy and low maintenance costs. Fourth, its overall economic advantages make it suitable for small-scale applications. Fifth, it eliminates the risk of liquid drift when used as an energy tower. Sixth, the energy consumption for coupled compression enthalpy enhancement is further reduced.

[0069] The above are merely preferred embodiments of the present invention, but the scope of protection of the present invention is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A gas-liquid heat and mass exchange and separation system, characterized in that, It comprises: a feed pipe group; a supergravity device (6), the gas inlet of the supergravity device (6) and / or the liquid inlet of the supergravity device (6) is connected with the feed pipe group; an air outlet pipe (32), which is connected with the air outlet of the supergravity device (6); a liquid outlet pipe (34), which is connected with the liquid outlet of the supergravity device (6).

2. The gas-liquid heat and mass transfer and separation system of claim 1, wherein, It further comprises: a plurality of heat exchange devices, at least one of which is installed between the air outlet pipe (32) and the supergravity device (6), and at least one of which is installed between the liquid outlet pipe (34) and the supergravity device (6).

3. The gas-liquid heat and mass transfer and separation system of claim 2, wherein, The feed pipe group comprises: an inlet and outlet pipe (33), which is connected with the liquid inlet of the supergravity device (6), and at least one of the heat exchange devices is installed between the inlet and outlet pipe (33) and the supergravity device (6); an air inlet pipe (35), which is connected with the gas inlet of the supergravity device (6).

4. The gas-liquid heat and mass transfer and separation system of claim 1, wherein, It further comprises: a first pipeline (37), one end of which is connected with the supergravity device (6), and the other end of which is connected with the air outlet pipe (32); a first compressor (7), which is installed on the first pipeline (37).

5. The gas-liquid heat and mass transfer and separation system of claim 1, wherein, It further comprises: a gas-liquid separator (5), the liquid inlet of which is connected with the liquid outlet of the supergravity device (6); a second pipeline (38), one end of which is connected with the supergravity device (6), and the other end of which is connected with the gas-liquid separator (5); a second compressor (8), which is installed on the second pipeline (38).

6. The gas-liquid heat and mass transfer and separation system of claim 5, wherein, It further comprises: a third pipeline (39), one end of which is connected with the gas-liquid separator (5); a pump (10), which is installed on the third pipeline (39); a fourth pipeline (40), one end of which is connected with the gas-liquid separator (5) after passing through the heat exchange device between the air outlet pipe (32) and the supergravity device (6), and the other end of which is connected with the liquid outlet pipe (34), and the other end of the third pipeline (39) is connected with the middle part of the fourth pipeline (40).

7. The gas-liquid heat and mass transfer and separation system of claim 3, wherein, It further comprises: a fifth pipeline (41), one end of which is connected with the liquid inlet of the supergravity device (6), and the other end of which is connected with the inlet and outlet pipe (33); a sixth pipeline (42), one end of which is connected with the air outlet of the supergravity device (6), and the other end of which is connected with the inlet and outlet pipe (33).

8. The gas-liquid heat and mass transfer and separation system of claim 7, wherein, It further comprises: a seventh pipeline (43), one end of which is connected with the liquid inlet of the supergravity device (6), and the second end of which is connected with the middle part of the sixth pipeline (42); A liquid inlet pipe (36) is connected with the middle part of the seventh pipeline (43).

9. The gas-liquid heat and mass transfer and separation system of claim 3, wherein, Further comprising: An eighth pipeline (44) is connected with the mechanical seal bearing inlet and outlet circulating water connection system of the super gravity device (6) at one end; A first heat exchanger (1) is connected with the other end of the eighth pipeline (44); A working medium circulation pipeline (46) is sequentially arranged on the heat exchange device on the inlet and outlet pipe (33), the first heat exchanger (1) and the heat exchange device between the liquid outlet pipe (34) and the super gravity device (6); A ninth pipeline (45) is connected with the working medium circulation pipeline (46) at both ends; A third compressor (9) is installed on the ninth pipeline (45), the first end of the working medium circulation pipeline (46) is connected with one end of the third compressor (9), and the second end of the working medium circulation pipeline (46) is connected with the other end of the third compressor (9).

10. The gas-liquid heat and mass transfer and separation system according to any one of claims 5 or 6, wherein, Further comprising: A liquid level meter (31) is installed on the gas-liquid separator (5).

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