A separation device for gas-liquid phase transition

Abstract

This invention relates to the field of gas-liquid phase transition separation technology, and proposes a separation device for gas-liquid phase transition. It includes a frame, a vortex enrichment mechanism, a liquefaction mechanism, a solid-liquid separation mechanism, and a liquid-liquid separation mechanism. The vortex enrichment mechanism is mounted on the frame, and the vortex enrichment mechanism, liquefaction mechanism, solid-liquid separation mechanism, and liquid-liquid separation mechanism are connected sequentially. The vortex enrichment mechanism includes a vortex coil with multiple through channels along the vortex direction, separated by filter plates. The through channels include a main channel, an inner centrifugal channel, an outer centrifugal channel, an upper gravity channel, and a lower gravity channel, with the outer centrifugal channel and inner centrifugal channel located on opposite sides of the main channel. This invention solves the problem of difficulty in fractionally separating dichloromethane mixtures in related technologies.

Description

Technical Field

[0001] This invention relates to the field of gas-liquid phase transition separation technology, and more specifically, to a separation device for gas-liquid phase transition. Background Technology

[0002] Dichloromethane is an organic compound with the chemical formula CH₂Cl₂. It is a colorless, transparent liquid with a pungent odor similar to ether. It is slightly soluble in water and soluble in ethanol and diethyl ether. Under normal operating conditions, it is a non-flammable, low-boiling-point solvent. Its vapor only produces a weakly combustible mixture when it reaches a high concentration in high-temperature air. It is often used to replace flammable petroleum ether and diethyl ether. Dichloromethane is generated in many industrial production lines, making the recovery of dichloromethane gas extremely important.

[0003] Current recovery technologies involve venting a mixture of dichloromethane and air outside the workshop via pipelines. The concentration of dichloromethane in the mixture is increased through adsorption and desorption using charcoal. This high-concentration dichloromethane mixture is then condensed into a liquid in a condenser, stored, filtered, and recycled. However, this process is costly due to several drawbacks. First, the equipment is bulky and expensive. Second, operating costs are high, requiring significant industrial heat and cooling. Heat is used for desorption, resulting in high-temperature dichloromethane gas; cooling is used to liquefy the gaseous dichloromethane. Third, the charcoal canisters have a lifespan of only two years, and replacing the charcoal is costly. In short, dichloromethane gas recovery equipment is expensive to invest in, energy-intensive, and difficult to classify and separate, hindering enterprise development. Therefore, there is an urgent need for a low-cost, low-energy-consumption device to achieve the classification, separation, and recovery of dichloromethane gas. Summary of the Invention

[0004] This invention proposes a separation device for gas-liquid phase transition, which solves the problem of difficulty in fractionally separating dichloromethane mixed gas in related technologies.

[0005] The technical solution of the present invention is as follows:

[0006] A separation device for gas-liquid phase transition includes a frame, a vortex enrichment mechanism, a liquefaction mechanism, a solid-liquid separation mechanism, and a liquid-liquid separation mechanism. The vortex enrichment mechanism is mounted on the frame, and the vortex enrichment mechanism, the liquefaction mechanism, the solid-liquid separation mechanism, and the liquid-liquid separation mechanism are connected sequentially. The vortex enrichment mechanism includes a vortex coil with multiple through channels along the spiral direction, which are separated by filter plates. Each through channel includes a main channel, an inner centrifugal channel, an outer centrifugal channel, an upper gravity channel, and a lower gravity channel. The upper gravity channel is located vertically above the inner centrifugal channel, and the lower gravity channel is located vertically below the outer centrifugal channel. The outlet of each through channel is connected to the liquefaction mechanism.

[0007] As a further technical solution

[0008] The vortex enrichment mechanism also includes a circulating fan and a makeup air fan, which are mounted on the vortex coil and connected to the main channel.

[0009] As a further technical solution

[0010] The liquefaction mechanism includes a liquefaction tank, an air inlet pipe, a honeycomb gas diffuser box, and a waterproof and breathable membrane. The air inlet pipe is connected to the outlet of the through channel. The liquefaction tank has the liquefied liquid outlet. The honeycomb gas diffuser box is disposed inside the liquefaction tank. The air inlet pipe is disposed through the liquefaction tank. The inlet of the air inlet pipe is connected to the outlet of the through channel. The outlet of the air inlet pipe is connected to the honeycomb gas diffuser box. The waterproof and breathable membrane is disposed inside the honeycomb gas diffuser box.

[0011] As a further technical solution

[0012] It also includes a low-concentration gas separation port in the upper gravity channel; a liquefied gas outlet on the liquefied tank; and a low-concentration merging channel connected to the low-concentration gas separation port and the liquefied gas outlet, wherein the low-concentration merging channel has an overflow port.

[0013] As a further technical solution

[0014] The solid-liquid separation mechanism includes a separation chamber and a filter element. The separation chamber has a separation inlet and a separation outlet. The filter element is disposed inside the separation chamber. The separation inlet is connected to the liquefied liquid outlet, and the separation outlet is connected to the liquid-liquid separation mechanism.

[0015] As a further technical solution

[0016] It also includes a heat exchange mechanism, which includes a condenser, an evaporator and a compressor. The condenser and the evaporator are both connected to the compressor. The condenser is connected to the liquid-liquid separation mechanism and the evaporator is connected to the liquefaction tank.

[0017] As a further technical solution

[0018] The liquid-liquid separation mechanism includes a separating tank, an inner liquid-collecting tube, and an outer liquid-collecting tube. The separating tank is internally divided into a mixed liquid area and an extractable liquid area. The inner liquid-collecting tube is vertically installed inside the separating tank and communicates with the extractable liquid area. The outer liquid-collecting tube is sleeved outside the inner liquid-collecting tube and has a through hole that communicates with the inner liquid-collecting tube. The separating tank has an inlet, a outlet, and a drain outlet. The inlet is located in the mixed liquid area and connected to the separation outlet. The outlet is located in the mixed liquid area and the drain outlet is located in the extractable liquid area. The height of the outlet is higher than the height of the inlet of the inner liquid-collecting tube.

[0019] As a further technical solution, it also includes

[0020] The mounting hole is located on the liquid separator and is used to connect the condenser.

[0021] As a further technical solution, it also includes

[0022] There are multiple partitions, which are staggered and arranged inside the liquid distribution tank to form a serpentine passage.

[0023] As a further technical solution, it also includes

[0024] Pressure balance port, which is located on the liquid distribution tank.

[0025] The working principle and beneficial effects of this invention are as follows: When the mixed gas enters the main channel, due to the higher density of dichloromethane in the mixed gas, the mixed gas diffuses from the main channel through the filter plate into the inner and outer centrifugal channels adjacent to the main channel. This diffusion phenomenon is not caused by external forces (such as convection or gravity) nor is it the result of a chemical reaction, but rather by the random motion of gas molecules. The mixed gas circulating within the vortex coil is subjected to centrifugal force. The mixed gas with a higher dichloromethane content in the main channel enters the outer centrifugal channel, while the mixed gas with a lower dichloromethane content enters the inner centrifugal channel. Thus, the first-stage separation of the mixed gas is completed. Since the upper gravity channel is located on the vertically extending upward side of the inner centrifugal channel, and the lower gravity channel is located on the vertically downward side of the outer centrifugal channel, the mixed gas with a high dichloromethane content after primary separation, under the influence of gravity, enters the lower gravity channel through the filter plate, while the mixed gas with a low dichloromethane content enters the upper gravity channel through the filter plate. Because the vortex coil is disc-shaped, the mixed gas circulating within it is subjected to centrifugal force. Therefore, the dichloromethane in the mixed gas located in the lower gravity channel tends to adhere to the outer side of the upper gravity channel. The outlet of the lower gravity channel is connected to the liquefaction mechanism, entering the next stage of separation. In this way, the function of staged separation of the dichloromethane mixed gas is achieved. Attached Figure Description

[0026] The present invention will now be described in further detail with reference to the accompanying drawings and specific embodiments.

[0027] Figure 1 This is a schematic diagram of a separation device for gas-liquid phase transition according to the present invention;

[0028] Figure 2 This is a schematic diagram of the vortex concentration mechanism of the present invention;

[0029] Figure 3 Appendix to this invention Figure 2 Enlarged cross-sectional view at point A in the middle;

[0030] Figure 4 This is a schematic diagram of the liquefaction mechanism of the present invention;

[0031] Figure 5 This is a schematic diagram of the solid-liquid separation mechanism of the present invention;

[0032] Figure 6 This is a schematic diagram of the liquid-liquid separation mechanism of the present invention;

[0033] Figure 7 This is a schematic cross-sectional view (C) of the liquid-liquid separation mechanism of the present invention;

[0034] Figure 8 This is a schematic cross-sectional view (B) of the liquid-liquid separation mechanism of the present invention;

[0035] Figure 9 This is a schematic diagram of the heat exchange mechanism of the present invention.

[0036] In the diagram: 1. Frame, 2. Vortex coil, 3. Filter plate, 4. Main channel, 5. Inner centrifugal channel, 6. Outer centrifugal channel, 7. Upper gravity channel, 8. Lower gravity channel, 9. Circulating fan, 10. Make-up air fan, 11. Liquefaction tank, 12. Inlet pipe, 13. Honeycomb gas diffuser, 14. Waterproof and breathable membrane, 15. Liquefied liquid outlet, 16. Low-concentration gas separation port, 17. Liquefied gas outlet, 18. Low-concentration confluence channel, 19. Overflow port, 20. Separation tank, 21. Filter element, 22. Separation inlet, 23. Separation outlet, 24. Condenser 25. Evaporator, 26. Compressor, 27. Liquid separator, 28. Inner liquid inlet pipe, 29. Outer liquid inlet pipe, 30. Mixed liquid zone, 31. Extracted liquid zone, 32. Through hole, 33. Liquid inlet, 34. Drain outlet, 35. Liquid outlet, 36. Mounting hole, 37. Baffle plate, 38. Pressure balance port, 39. Circulating air valve, 40. Make-up air valve, 41. Ball valve, 42. Y-type filter, 43. Vortex concentration mechanism, 44. Liquefaction mechanism, 45. Solid-liquid separation mechanism, 46. Liquid-liquid separation mechanism, 47. Heat exchange mechanism, 48. Liquefied gas pipeline. Detailed Implementation

[0037] The technical solutions of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0038] like Figures 1-9 As shown, this embodiment proposes a separation device for gas-liquid phase transition, including a frame 1, a vortex enrichment mechanism 43, a liquefaction mechanism 44, a solid-liquid separation mechanism 45, and a liquid-liquid separation mechanism 46. The vortex enrichment mechanism 43 is mounted on the frame 1, and the vortex enrichment mechanism 43, the liquefaction mechanism 44, the solid-liquid separation mechanism 45, and the liquid-liquid separation mechanism 46 are connected in sequence. The vortex enrichment mechanism 43 includes a vortex coil 2, which has multiple through channels along the spiral direction. The multiple through channels are separated by filter plates 3. The through channels include a main channel 4, an inner centrifugal channel 5, an outer centrifugal channel 6, an upper gravity channel 7, and a lower gravity channel 8. The upper gravity channel 7 is located above the inner centrifugal channel 5 in the vertical direction, and the lower gravity channel 8 is located below the outer centrifugal channel 6 in the vertical direction. The outlet of the through channels is connected to the liquefaction mechanism 44.

[0039] In this embodiment, when the mixed gas enters the main channel 4, due to the higher density of dichloromethane in the mixed gas, the mixed gas diffuses from the main channel 4 through the filter plate 3 into the inner centrifugal channel 5 and the outer centrifugal channel 6 adjacent to the main channel 4. This diffusion phenomenon is not caused by external forces (such as convection or gravity) nor is it a result of a chemical reaction, but rather by the random motion of gas molecules. The mixed gas circulating within the vortex coil 2 is subjected to centrifugal force. The mixed gas with a higher dichloromethane content in the main channel 4 enters the outer centrifugal channel 6, while the mixed gas with a lower dichloromethane content enters the inner centrifugal channel 5. Thus, the first-stage separation of the mixed gas is completed. Since the upper gravity channel 7 is located on the vertically extending upward side of the inner centrifugal channel 5, and the lower gravity channel 8 is located on the vertically downward side of the outer centrifugal channel 6, the mixed gas with a high dichloromethane content after primary separation, under the influence of gravity, enters the lower gravity channel 8 through the filter plate 3, while the mixed gas with a low dichloromethane content enters the upper gravity channel 7 through the filter plate 3. Because the vortex coil 2 is disc-shaped, the mixed gas circulating within it is subjected to centrifugal force. Therefore, the dichloromethane in the mixed gas located in the lower gravity channel 8 tends to adhere to the outer side of the upper gravity channel 7. The outlet of the lower gravity channel 8 is connected to the liquefaction mechanism 44, entering the next stage of separation. In this way, the function of staged separation of the dichloromethane mixed gas is achieved.

[0040] like Figure 2 As shown, further, it also includes,

[0041] The vortex enrichment mechanism 43 also includes a circulating fan 9 and a makeup air fan 10. The makeup air fan 10 and the circulating fan 9 are mounted on the vortex coil 2 and are connected to the main channel 4.

[0042] In this embodiment, a circulating fan 9 and a makeup air fan 10 are connected to the main channel 4, and corresponding circulating air valves 39 and makeup air valves 40 are provided. When the mixed gas enters the main channel 4, the circulating fan 9 drives the mixed gas to circulate in the main channel 4. The circulating air valve 39 can control the mixed gas to enter the vortex coil 2. When the mixed gas enters the next stage separation mechanism after being separated in the vortex coil 2, if the entry rate of the original mixed gas is lower than that of the vortex coil 2 in conveying the separated mixed gas to the next stage, the vortex coil 2 will generate negative pressure, which is not conducive to the separation work of the vortex coil 2. At this time, the mixed gas of dichloromethane and air inside the equipment enters the vortex coil 2 from the makeup air fan 10 through the makeup air valve 40 to eliminate the negative pressure generated, and so on.

[0043] like Figure 4 As shown, further, it also includes,

[0044] The liquefaction mechanism 44 includes a liquefaction tank 11, an air inlet pipe 12, a honeycomb gas diffuser box 13, and a waterproof and breathable membrane 14. The air inlet pipe 12 is connected to the outlet of the through channel. The liquefaction tank 11 has a liquefied liquid outlet 15. The honeycomb gas diffuser box 13 is disposed inside the liquefaction tank 11. The air inlet pipe 12 is disposed through the liquefaction tank 11. The inlet of the air inlet pipe 12 is connected to the outlet of the through channel. The outlet of the air inlet pipe 12 is connected to the honeycomb gas diffuser box 13. The waterproof and breathable membrane 14 is disposed inside the honeycomb gas diffuser box 13.

[0045] In this embodiment, the liquefaction mechanism 44 includes a liquefaction tank 11, an air inlet pipe 12, a honeycomb gas diffuser box 13, and a waterproof and breathable membrane 14. The air inlet pipe 12 is disposed through the liquefaction tank 11, and its inlet is connected to the outlet of the through channel. The dichloromethane mixture gas, after preliminary separation by the vortex coil 2, enters the liquefaction tank 11 through the air inlet pipe 12. The honeycomb gas diffuser box 13 is disposed inside the liquefaction tank 11, and its outlet is connected to the honeycomb gas diffuser box 13. The dichloromethane mixture gas enters the honeycomb gas diffuser box 13 through the air inlet pipe 12. The waterproof and breathable membrane 14 is disposed in the honeycomb gas diffuser box 13. Inside, the dichloromethane mixture is dispersed by the honeycomb diffuser box 13, then passes through the waterproof and breathable membrane 14 into the liquefaction tank 11. At the bottom of the liquefaction tank 11, there is a portion of low-temperature dichloromethane liquid. The dichloromethane mixture immediately comes into contact with this liquid, causing it to rapidly cool down. The dichloromethane in the mixture liquefies and merges with the existing low-temperature dichloromethane liquid in the liquefaction tank 11. Water molecules in the mixture condense into ice particles that float on the surface of the liquid dichloromethane. The remaining portion of the mixture with low dichloromethane content is discharged through the outlet on the liquefaction tank 11. The liquefaction tank 11 has a liquefied liquid outlet 15, through which the mixture of dichloromethane and ice particles is discharged into the next stage separation mechanism.

[0046] like Figure 2 , Figure 4 As shown, further, it also includes,

[0047] It also includes a low-concentration gas separation port 16 in the upper gravity channel 7; a liquefied gas outlet 17 on the liquefied tank 11; and a low-concentration confluence channel 18 connected to the low-concentration gas separation port 16 and the liquefied gas outlet 17, with an overflow port 19 on the low-concentration confluence channel 18.

[0048] In this embodiment, the upper gravity channel 7 inside the vortex coil 2 has a low-concentration gas separation port 16 for discharging the mixed gas with low dichloromethane content after primary separation; the liquefaction tank 11 has a liquefied gas outlet 17 for discharging the remaining mixed gas with low dichloromethane content after passing through the low-temperature dichloromethane liquid in the liquefaction mechanism 44; the low-concentration gas separation port 16 is connected to a low-concentration confluence channel 18, and the liquefied gas outlet 17 is connected to the low-concentration confluence channel 18 through a liquefied gas pipe 48; the low-concentration confluence channel 18 has an overflow port 19, and the mixed gas with low dichloromethane content after separation by the vortex coil 2 and the liquefaction mechanism 44 is discharged from the overflow port 19 and enters the relevant dichloromethane production line to absorb new dichloromethane gas, which is then re-entered into this separation device as the dichloromethane mixed gas to be processed.

[0049] like Figure 5 As shown, further, it also includes,

[0050] The solid-liquid separation mechanism 45 includes a separation chamber 20 and a filter element 21. The separation chamber 20 has a separation inlet 22 and a separation outlet 23. The filter element 21 is disposed inside the separation chamber 20. The separation inlet 22 is connected to the liquefied liquid outlet 1517, and the separation outlet 23 is connected to the liquid-liquid separation mechanism 46.

[0051] In this embodiment, the mixture of dichloromethane and ice particles separated by the liquefaction mechanism 44 enters the separation mechanism through the separation inlet 22 on the separation box 20. The filter element 21 is located inside the separation box 20. The suspension of dichloromethane and ice particles enters the filter element 21. After being filtered by the filter element 21, the high-concentration dichloromethane mixture flows out from the separation outlet 23. The separation outlet 23 is connected to the liquid-liquid separation mechanism 46, and the high-concentration dichloromethane mixture enters the liquid-liquid separation mechanism 46.

[0052] like Figure 9 As shown, further, it also includes,

[0053] It also includes a heat exchange mechanism 47, which includes a condenser 24, an evaporator 25 and a compressor 26. The condenser 24 and the evaporator 25 are both connected to the compressor 26. The condenser 24 is connected to the liquid-liquid separation mechanism 46 and the evaporator 25 is connected to the liquefaction tank 11.

[0054] In this embodiment, the evaporator 25 is connected to the liquefaction tank 11 and is used to cool the separation tank 20 to maintain liquid dichloromethane; the condenser 24 is connected to the liquid-liquid separation mechanism 46 and is used to heat the liquid-liquid separation mechanism 46.

[0055] like Figures 6-8 As shown, further, it also includes,

[0056] The liquid-liquid separation mechanism 46 includes a liquid separation tank 27, an inner liquid collection tube 28, and an outer liquid collection tube 29. The liquid separation tank 27 is internally divided into a mixed liquid area 30 and an extract liquid area 31. The inner liquid collection tube 28 is vertically installed inside the liquid separation tank 27 and communicates with the extract liquid area 31. The outer liquid collection tube 29 is sleeved outside the inner liquid collection tube 28 and has a through hole 32 that communicates with the inner liquid collection tube 28. The liquid separation tank 27 has a liquid inlet 33, a drain outlet 34, and a discharge outlet 35. The liquid inlet 33 is located in the mixed liquid area 30 and connected to the separation outlet 23. The drain outlet 34 is located in the mixed liquid area 30, and the discharge outlet 35 is located in the extract liquid area 31. The height of the drain outlet 34 is higher than the height of the inlet of the inner liquid collection tube 28.

[0057] In this embodiment, the high-concentration dichloromethane mixture after filtration by the solid-liquid separation mechanism 45 still contains a small amount of ice particles. The high-concentration dichloromethane mixture enters the liquid-liquid separator through the inlet 33 on the separating tank 27 for further separation. As the high-concentration dichloromethane mixture enters the separating tank 27, the condenser 24 of the heat exchange mechanism 47 heats the mixture, melting the ice particles. Because dichloromethane solution and water are poorly soluble, stratification occurs. As the stratified layers rise, the dichloromethane liquid at the bottom flows through the through-hole 32 on the bottom outer liquid-taking pipe 29 into the inner pipe of the bottom liquid-taking pipe, and then into the extraction liquid zone 31 of the separating tank 27. At this point, a relatively pure dichloromethane solution has been recovered. This solution is then sent to the production line for recycling through the ball valve 41 and the Y-type filter 42, while the water flows out through the drain outlet 34 on the separating tank 27.

[0058] like Figure 8 As shown, further, it also includes,

[0059] Mounting hole 36, located on the liquid separator 27, is used to connect the condenser 24.

[0060] In this embodiment, the mounting hole 36 on the liquid separator 27 is used to connect the condenser 24 for heating the high-concentration dichloromethane mixture, so that the ice particles in the high-concentration dichloromethane mixture melt quickly.

[0061] like Figure 8 As shown, further, it also includes,

[0062] There are multiple partitions 37, which are staggered and arranged inside the liquid distribution tank 27 to form a serpentine passage.

[0063] In this embodiment, multiple baffles 37 are staggered inside the liquid separation tank 27 to form a serpentine passage. Through the flow channel formed by the baffles 37, the high-concentration dichloromethane mixture gradually tends to flow horizontally, which is beneficial to the subsequent separation work.

[0064] like Figure 6 As shown, further, it also includes,

[0065] Pressure balance port 38 is located on the liquid distribution tank 27.

[0066] In this embodiment, the condenser 24 is used to heat the high-concentration dichloromethane mixture in the liquid separator 27. Due to the principle of thermal expansion and contraction, a pressure difference will be formed inside and outside the liquid separator 27, which is not conducive to liquid separation. Therefore, a pressure balance port 38 is added. The pressure balance port 38 is located on the liquid separator 27, which effectively solves the problem of pressure difference inside the liquid separator.

[0067] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A separation device for gas-liquid phase transition, characterized in that, The system includes a frame (1), a vortex concentration mechanism (43), a liquefaction mechanism (44), a solid-liquid separation mechanism (45), and a liquid-liquid separation mechanism (46). The vortex concentration mechanism (43) is mounted on the frame (1), and the vortex concentration mechanism (43), the liquefaction mechanism (44), the solid-liquid separation mechanism (45), and the liquid-liquid separation mechanism (46) are connected in sequence. The vortex concentration mechanism (43) includes a vortex coil (2), which has multiple through channels along the vortex direction. The through channels are separated by filter plates (3); the through channels include a main channel (4), an inner centrifugal channel (5), an outer centrifugal channel (6), an upper gravity channel (7) and a lower gravity channel (8). The outer centrifugal channel (6) and the inner centrifugal channel (5) are located on both sides of the main channel (4). The upper gravity channel (7) is located on the upper vertical direction of the inner centrifugal channel (5). The lower gravity channel (8) is located on the lower vertical direction of the outer centrifugal channel (6). The outlet of the through channel is connected to the liquefaction mechanism.

2. The separation device for gas-liquid phase transition according to claim 1, characterized in that, The vortex enrichment mechanism (43) also includes a circulating fan (9) and a makeup air fan (10), which are mounted on the vortex coil (2) and connected to the main channel (4).

3. The separation device for gas-liquid phase transition according to claim 1, characterized in that, The liquefaction mechanism (44) includes a liquefaction tank (11), an air inlet pipe (12), a honeycomb gas diffuser (13), and a waterproof and breathable membrane (14). The air inlet pipe (12) is connected to the outlet of the through channel. The liquefaction tank (11) has a liquefied liquid outlet (15). The honeycomb gas diffuser (13) is located inside the liquefaction tank (11). The air inlet pipe (12) is installed through the liquefaction tank (11). The inlet of the air inlet pipe (12) is connected to the outlet of the through channel. The outlet of the air inlet pipe (12) is connected to the honeycomb gas diffuser (13). The waterproof and breathable membrane (14) is located inside the honeycomb gas diffuser (13).

4. A separation device for gas-liquid phase transition according to claim 3, characterized in that, The upper gravity channel (7) has a low-concentration gas separation port (16); the liquefaction tank (11) has a liquefied gas outlet (17); a low-concentration confluence channel (18) is connected between the low-concentration gas separation port (16) and the liquefied gas outlet (17), and the low-concentration confluence channel (18) has an overflow port (19).

5. A separation device for gas-liquid phase transition according to claim 3, characterized in that, The solid-liquid separation mechanism (45) includes a separation chamber (20) and a filter element (21). The separation chamber (20) has a separation inlet (22) and a separation outlet (23). The filter element (21) is located inside the separation chamber (20). The separation inlet (22) is connected to the liquefied liquid outlet (15), and the separation outlet (23) is connected to the liquid-liquid separation mechanism (46).

6. A separation device for gas-liquid phase transition according to claim 5, characterized in that, It also includes a heat exchange mechanism (47), which includes a condenser (24), an evaporator (25) and a compressor (26). The condenser (24) and the evaporator (25) are connected to the compressor (26). The condenser (24) is connected to the liquid-liquid separation mechanism, and the evaporator (25) is connected to the liquefaction tank (11).

7. A separation device for gas-liquid phase transition according to claim 6, characterized in that, The liquid-liquid separation mechanism (46) includes a liquid separation tank (27), an inner liquid collection tube (28), and an outer liquid collection tube (29). The liquid separation tank (27) is internally divided into a mixed liquid area (30) and an extract liquid area (31). The inner liquid collection tube (28) is vertically installed inside the liquid separation tank (27) and is connected to the extract liquid area (31). The outer liquid collection tube (29) is sleeved outside the inner liquid collection tube (28) and has a through hole (32). The through hole (32) is connected to the liquid collection inner tube (28). The liquid separation tank (27) has a liquid inlet (33), a drain outlet (34) and a drain outlet (35). The liquid inlet (33) is located in the mixed liquid area (30) and connected to the separation outlet (23). The drain outlet (34) is located in the mixed liquid area (30). The drain outlet (35) is located in the extract liquid area (31). The height of the drain outlet (34) is higher than the height of the inlet of the liquid collection inner tube (28).

8. A separation device for gas-liquid phase transition according to claim 7, characterized in that, Also includes Mounting hole (36), located on the liquid separator (27), is used to connect the condenser (24).

9. A separation device for gas-liquid phase transition according to claim 7, characterized in that, Also includes There are multiple partitions (37), which are staggered inside the liquid distribution tank (27) to form a serpentine passage.

10. A separation device for gas-liquid phase transition according to claim 7, characterized in that, Also includes Pressure balance port (38) is located on the liquid separator (27).

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