Raw gas condensing separation device with cold recovery and method of use thereof

Abstract

The application discloses a raw material gas condensing separation device with cold energy recovery and a use method thereof, which comprises a shell, wherein the shell is a barrel-shaped structure with an arc-shaped bottom surface, a low-temperature liquid inlet and outlet are arranged at the center of the bottom of the shell, a gas discharge port is arranged at the center of the upper cover of the top of the shell, the upper cover of the shell is further provided with a low-temperature gas inlet, a low-pressure adjusting valve, a low-temperature gas outlet, a raw material gas inlet, a normal-temperature ultra-pure gas outlet, a low-temperature ultra-pure gas inlet, a low-temperature pure gas outlet, a high-pressure adjusting valve, and the device is more compact in structure, higher in heat transfer efficiency and safer in operation, the method is simple and applicable, and the application range is wider; since the adsorber is separated, the adsorber equipment is smaller and more compact, the consumption of regeneration gas and liquid nitrogen is reduced, and the product yield is improved; the gas phase recovery after two-stage throttling improves the product yield; the cold energy of the ultra-pure gas and the cold energy of the low-temperature liquid evaporated during subsequent low-temperature adsorption are fully recovered, and the energy consumption is saved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of cryogenic technology, and in particular to a raw material gas condensing and separating device with cold energy recovery. BACKGROUND

[0002] Rare gases are increasingly widely used. For example, ultrapure helium is widely used in the manufacturing fields of aerospace, medicine, metallurgy, semiconductors, reactors, superconductors, etc., and is a strategic resource related to national defense security. For example, ultrapure hydrogen is widely used in the fields of electronics industry, float glass production, metallurgical industry, aerospace, etc.

[0003] The low-temperature condensing separation and purification method is a method for obtaining ultrapure products by cooling normal-temperature gas to 77-85K, condensing high-boiling-point components such as N2, CO and CH4, and separating them in a gas-liquid separator, and then through a low-temperature adsorber. It is the most mature technology, the highest product recovery rate, and the smallest investment and operation cost of ultrapure gas purification method. The low-temperature purifier adopts the HG / T5996-2022 standard integrated equipment. This equipment is mainly used for devices with small processing capacity and intermittent operation. For devices with large processing capacity and continuous operation, there are problems of large equipment, large consumption of regeneration gas and low-temperature liquid, and low product yield. The present application separates the low-temperature condensing separation and the low-temperature adsorption in two devices, and is aimed at the front-end low-temperature condensing separation. SUMMARY

[0004] In order to overcome the shortcomings of the prior art, the present application provides a raw material gas condensing and separating device with cold energy recovery, which solves the problems of large equipment, large consumption of regeneration gas and low-temperature liquid, and low product yield for devices with large processing capacity and continuous operation.

[0005] A raw material gas condensing and separating device with cold energy recovery, comprising a shell, the shell is a barrel-shaped structure with an arc-shaped bottom surface, a low-temperature liquid inlet and outlet are arranged at the center of the bottom of the shell, a gas discharge port is arranged at the center of the upper cover of the top of the shell, a low-temperature gas inlet, a low-pressure regulating valve, a low-temperature gas outlet, a raw material gas inlet, a normal-temperature ultrapure gas outlet, a low-temperature ultrapure gas inlet, a low-temperature pure gas outlet and a high-pressure regulating valve are further arranged on the upper cover of the shell.

[0006] The low-temperature gas inlet is connected with the low-temperature gas outlet through a pipeline, and the low-temperature gas outlet is arranged in the middle of the shell.

[0007] The outlet of the low-pressure regulating valve is connected with the outlet of the low-pressure regulating valve at the bottom of the shell through a pipeline, and the inlet is connected with the liquid outlet of the low-pressure separator. The liquid outlet of the low-pressure separator is located at the bottom of the low-pressure separator. A liquid inlet of the low-pressure separator is further arranged on the low-pressure separator and connected to the high-pressure regulating valve through a pipeline. A gas outlet of the low-pressure separator is arranged at the top end of the low-pressure separator and connected with the low-temperature gas outlet through a pipeline.

[0008] The upper end of the raw material gas inlet is connected with an upper distributor, the lower end of the upper distributor is arranged in an upper collector, the upper collector is connected with a normal-temperature ultra-pure gas outlet through a pipeline, the lower end of the upper collector is arranged with a coiled tube type condenser heat exchanger, the lower end of the coiled tube type condenser heat exchanger is arranged with a lower distributor, the lower distributor is connected with a low-temperature ultra-pure gas inlet through a pipeline, the lower end of the lower distributor is arranged with a lower collector, and the lower end of the lower collector is connected with a cooling coil through a pipeline.

[0009] The low-temperature pure gas outlet is connected with a high-pressure separator low-temperature pure gas outlet through a pipeline, the low-temperature pure gas outlet is arranged on the high-pressure separator, a high-pressure separator inlet is further arranged in the middle of the high-pressure separator and connected with the cooling coil, a high-pressure separator liquid outlet is arranged at the bottom of the high-pressure separator and connected with a high-pressure regulating valve through a pipeline.

[0010] Further, the cylinder and the lower head of the shell are a multi-layer vacuum insulation or vacuum powder insulation Dewar structure, which can also be designed as a single-layer outer shell with external insulation; the upper cover can be a flat cover connected by a flange or an elliptical, butterfly-shaped or other type of head.

[0011] Further, the low-pressure regulating valve and the high-pressure regulating valve are fixed on the upper cover, the valve body is located in the shell, and the actuator is arranged outside the shell, so that the valve core can be repaired, replaced or operated outside the device without disassembling or breaking the shell.

[0012] Further, the coiled tube type condenser heat exchanger is a double-pipe coiled tube heat exchanger or a multi-pipe coiled heat exchanger, which realizes three-stream heat transfer or multi-stream heat transfer.

[0013] Further, the low-pressure separator and the high-pressure separator are arranged at the lower part of the coiled tube type condenser heat exchanger and immersed in the low-temperature liquid to realize the gas-liquid separation function.

[0014] Further, the lower distributor, the lower collector, the upper collector and the upper distributor are circular, arc or cylindrical pipelines, which realize the collection of multiple coiled tube gas streams or the distribution of gas streams to multiple coiled tubes.

[0015] Further, the cooling coil is wound outside the low-pressure separator and the high-pressure separator and immersed in the low-temperature liquid to further cool the medium in the coil to the temperature of the low-temperature liquid.

[0016] Further, the low-temperature liquid can be liquid nitrogen, liquid argon, liquid air, liquid neon or liquid helium.

[0017] Further, the use method comprises the following steps:

[0018] S1, the low-temperature liquid level in the device is controlled to be fully immersed in the low-pressure separator, the high-pressure separator, but not more than the lower distributor, and the low-temperature liquid operating temperature is-145℃~-243℃;

[0019] S2, the raw gas enters the upper distributor from the raw gas inlet, then enters the spiral wound condenser heat exchanger and is cooled to-145℃~-243℃ to obtain a gas-liquid mixture, then enters the lower collector for collection, is cooled to the low-temperature liquid temperature by the cooling coil, enters the high-pressure separator for gas-liquid separation, and the gas phase is discharged from the low-temperature pure gas outlet;

[0020] S3, the liquid phase of the high-pressure separator is throttled to 0.3~0.5MPa by the high-pressure regulating valve and then enters the low-pressure separator for gas-liquid separation, the gas phase is discharged from the device to the recovery system, and the liquid phase is throttled to the operating pressure of the low-temperature liquid in the device by the low-pressure regulating valve and is discharged to the bottom of the device to supplement the consumption of the low-temperature liquid;

[0021] S4, the ultra-pure gas enters the spiral wound condenser heat exchanger after being distributed by the lower distributor from the low-temperature ultra-pure gas inlet, provides cold energy for the spiral wound condenser heat exchanger (3), and the low-temperature ultra-pure gas is reheated and enters the upper collector (11) and is discharged from the normal-temperature ultra-pure gas outlet (1306);

[0022] S5, the low-temperature gas entering from the low-temperature gas inlet is mixed with the low-temperature liquid evaporation gas and passes through the gap between the outer shell and the spiral wound tube of the spiral wound condenser heat exchanger to provide cold energy for the spiral wound condenser heat exchanger, and the low-temperature gas is reheated to normal temperature and discharged from the device.

[0023] Further, the raw gas operating pressure is 2~20MPa, the impurity content of nitrogen, oxygen and the like is 20~95%, and the temperature is normal temperature.

[0024] Further, the high-pressure separator gas phase purity is 90~99.5%, the higher the raw gas pressure, the higher the purity, and the lower the immersed low-temperature liquid temperature, the higher the purity.

[0025] The beneficial effects of the present application are: the device structure is more compact, the heat transfer efficiency is higher, the operation is safer, the method is simple and applicable, and the application range is wider; because the adsorber is separated, the adsorber equipment is smaller and more compact, the regeneration gas and liquid nitrogen consumption is reduced, and the product yield is improved; the two-stage throttled gas phase is recovered, and the product yield is improved; the cold energy of the ultra-pure gas is fully recovered, the low-temperature liquid cold energy evaporated during subsequent low-temperature adsorption is recovered, and the energy consumption is saved. BRIEF DESCRIPTION OF DRAWINGS

[0026] Figure 1 It is a raw gas condensing separation device structure schematic diagram with cold energy recovery;

[0027] Figure: 1 - shell, 2 - low pressure regulating valve, 3 - coiled tube condenser heat exchanger, 4 - lower distributor, 5 - lower collector, 6 - low pressure separator, 7 - high pressure separator, 8 - cooling coil, 9 - flow guide, 10 - high pressure regulating valve, 11 - upper collector, 12 - upper distributor, 1301 - raw gas inlet, 1302 - high pressure separator inlet, 1303 - high pressure separator low temperature pure gas outlet, 1304 - low temperature pure gas outlet, 1305 - low temperature ultra-pure gas inlet, 1306 - normal temperature ultra-pure gas outlet, 1401 - high pressure separator liquid outlet, 1402 - low pressure separator inlet, 1403 - low pressure separator gas outlet, 1404 - low temperature gas outlet, 1501 - low pressure separator liquid outlet, 1502 - low pressure regulating valve outlet, 1601 - low temperature gas inlet, 1602 - low temperature gas outlet, 17 - gas discharge port, 18 - low temperature liquid inlet and outlet. DETAILED DESCRIPTION

[0028] The present application will now be described by way of specific embodiments, which are provided for illustration only, and should not be construed to limit the present application in any way. Although the present application will be described with reference to the preferred embodiments, it is to be understood that the present application is not limited to the preferred embodiments. Rather, the preferred embodiments are provided to illustrate the present application. To provide a thorough understanding of the present application, numerous specific details are set forth in the following description. The present application can be practiced without these specific details. In other instances, well-known methods have not been described in detail in order not to unnecessarily obscure the present application. In addition, in the interest of clarity, some of the drawings can not be to scale and are provided merely to conceptually illustrate the features of the present application. It should also be noted that where specific integers are shown in the drawings, these do not signify that the application is limited to these specific embodiments. In the description of the present application, like numbers refer to like objects in the drawings, and the following description is not limited to the drawings. It should be noted that the embodiments and features of the present application can be combined with each other, if not contradictory.

[0029] Unless otherwise defined, the technical or scientific terms used in this invention should be understood in their ordinary sense by one of ordinary skill in the art. The terms "first," "second," and similar terms used in this invention do not indicate any order, quantity, or importance, but are merely used to distinguish different components. Similarly, the terms "an" or "a" and similar terms do not indicate a quantity limitation, but rather indicate the presence of at least one. Terms such as "set," "connected," and "linked" should be interpreted broadly; for example, they can refer to a fixed connection, a detachable connection, or an integral connection; a mechanical connection or an electrical connection; a direct connection or an indirect connection through an intermediate medium; or a connection within two components. Those skilled in the art can understand the specific meaning of the above terms in this embodiment based on the specific circumstances. The directions or positional relationships indicated by terms such as "up," "down," "left," "right," "inner," and "bottom" are based on the directions or positional relationships shown in the accompanying drawings, or the directions or positional relationships that the product of the invention is usually placed in during use. They are only for the purpose of facilitating the description of the invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention.

[0030] To make the objectives, technical solutions, and advantages of the present invention clearer, the embodiments of the present invention will be described in further detail below with reference to the accompanying drawings.

[0031] In this embodiment, as shown in the appendix Figure 1 As shown, a raw material gas condensation and separation device with cold energy recovery includes a shell 1, which is a barrel-shaped structure with an arc-shaped bottom. A low-temperature liquid inlet and outlet 18 is provided at the center of the bottom. The top of the shell 1 is a top cover with a gas outlet 17 at the center. The top cover of the shell 1 is also provided with a low-temperature gas outlet 1601 located at the edge of the cover, a low-pressure regulating valve 2, a low-temperature gas outlet 1404, a raw material gas inlet 1301, a room temperature ultrapure gas outlet 1306, a low-temperature ultrapure gas inlet 1305, a low-temperature ultrapure gas inlet 1304, and a high-pressure regulating valve 10.

[0032] The cryogenic gas inlet 1601 is connected to the cryogenic gas outlet 1602 via a pipe, and the cryogenic gas outlet 1602 is located in the middle of the shell.

[0033] The low-pressure regulating valve 2 outlet is connected with the low-pressure regulating valve outlet 1502 at the bottom of the shell through a pipeline, and the inlet is connected with the low-pressure separator liquid outlet 1501, which is arranged at the bottom of the low-pressure separator 6. The low-pressure separator 6 is also provided with a low-pressure separator liquid inlet 1402 and is connected with the high-pressure regulating valve 10 through a pipeline. The top end of the low-pressure separator 6 is provided with a low-pressure separator gas outlet 1403 and is connected with a low-temperature gas outlet 1404 through a pipeline.

[0034] The raw material gas inlet 1301 is connected with the upper distributor 12 at the lower end. The upper distributor 12 is provided with an upper collector 11 at the lower end, which is connected with a normal-temperature ultra-pure gas outlet 1306 through a pipeline. The lower end of the upper collector 11 is provided with a coiled tube type condensation heat exchanger 3, and the lower part is provided with a lower distributor 4, which is connected with a low-temperature ultra-pure gas inlet 1305 through a pipeline. The lower end of the lower distributor 4 is provided with a lower collector 5, which is connected with a cooling coil 8 through a pipeline.

[0035] The low-temperature pure gas outlet 1304 is connected with the high-pressure separator low-temperature pure gas outlet 1303 through a pipeline. The low-temperature pure gas outlet 1303 is arranged on the high-pressure separator 7. The middle part of the high-pressure separator 7 is also provided with a high-pressure separator inlet 1302 and is connected with the cooling coil 8. The bottom of the high-pressure separator 7 is provided with a high-pressure separator liquid outlet 1401 and is connected with the high-pressure regulating valve 10 through a pipeline.

[0036] The cylinder and lower head of the shell 1 are in a multi-layer vacuum insulation or vacuum powder insulation Dewar structure, and can also be designed as a single-layer outer shell with external insulation. The upper cover can be a flat cover connected by a flange or an elliptical, butterfly-shaped or other type of head.

[0037] The low-pressure regulating valve 2 and the high-pressure regulating valve 10 are fixed on the upper cover, and the valve body is located in the shell 1. The actuator is arranged outside the shell 1, so that the valve core can be repaired, replaced and operated outside the device without disassembling or breaking the shell.

[0038] The coiled tube type condensation heat exchanger 3 is a double-pipe coiled tube heat exchanger or a multi-pipe parallel coiled heat exchanger, which realizes three-stream heat transfer or multi-stream heat transfer.

[0039] The low-pressure separator 6 and the high-pressure separator 7 are arranged at the lower part of the coiled tube type condensation heat exchanger 3 and are immersed in the low-temperature liquid to realize the gas-liquid separation function.

[0040] The lower distributor 4, the lower collector 5, the upper collector 11 and the upper distributor 12 are circular ring-shaped, arc-shaped or cylindrical pipelines, which realize the functions of collecting multiple coiled tube gas streams or distributing the gas stream to multiple coiled tubes.

[0041] The cooling coil 8 is wound outside the low-pressure separator 6 and the high-pressure separator 7 and is immersed in the low-temperature liquid, further cooling the medium in the coil to the temperature of the low-temperature liquid.

[0042] The low-temperature liquid can be liquid nitrogen, liquid argon, liquid air, liquid neon, liquid helium or the like.

[0043] The use method comprises the following steps:

[0044] S1, the liquid level of the low-temperature liquid in the device is controlled to be fully immersed in the low-pressure separator 6 and the high-pressure separator 7, but does not exceed the lower distributor 4, and the operating temperature of the low-temperature liquid is -145℃~-243℃;

[0045] S2, the raw gas enters the upper distributor 12 from the raw gas inlet 1301, then enters the coil condenser heat exchanger 3 and is cooled to -145℃~-243℃ to obtain a gas-liquid mixture, then enters the lower collector 5 for collection, is cooled to the temperature of the low-temperature liquid by the cooling coil 8, enters the high-pressure separator 7 for gas-liquid separation, and the gas phase is discharged through the low-temperature pure gas outlet 1304;

[0046] S3, the liquid phase of the high-pressure separator 7 is throttled to 0.3~0.5MPa by the high-pressure regulating valve 10, then enters the low-pressure separator 6 for gas-liquid separation, the gas phase is discharged from the device to the recovery system, and the liquid phase is throttled to the operating pressure of the low-temperature liquid in the device by the low-pressure regulating valve 2 and is discharged to the bottom of the device to supplement the consumption of the low-temperature liquid;

[0047] S4, the ultra-pure gas enters the coil condenser heat exchanger 3 after being distributed by the lower distributor 5 from the low-temperature ultra-pure gas inlet 1305, provides cold energy for the coil condenser heat exchanger 3, and the low-temperature ultra-pure gas is reheated and enters the upper collector 11 and is discharged from the normal-temperature ultra-pure gas outlet 1306;

[0048] S5, the low-temperature gas entering from the low-temperature gas inlet 1601 is mixed with the low-temperature liquid evaporation gas and passes through the gap between the outer shell and the coil of the coil condenser heat exchanger 3 to provide cold energy for the coil condenser heat exchanger 3, and the low-temperature gas and the ultra-pure gas are reheated to normal temperature and discharged from the device.

[0049] The operating pressure of the raw gas is 2~20MPa, the content of impurities such as nitrogen and oxygen is 20~95%, and the temperature is normal temperature.

[0050] The purity of the gas phase of the high-pressure separator 7 is 90~99.5%, the higher the pressure of the raw gas, the higher the purity, and the lower the temperature of the immersed low-temperature liquid, the higher the purity.

[0051] The application has the advantages of compact device structure, high heat transfer efficiency, safe operation, simple method, wide application range, small and delicate adsorber equipment due to separation from the adsorber, reduced consumption of regeneration gas and liquid nitrogen, and improved product yield; gas phase recovery after two-stage throttling improves the product yield; the cold energy of the ultra-pure gas and the cold energy of the low-temperature liquid evaporated during subsequent low-temperature adsorption are fully recovered, and energy consumption is saved.

[0052] The above shows and describes the basic principles and main features of the application and the advantages of the application. Those skilled in the art should understand that the application is not limited to the above examples, and the above examples and descriptions in the specification are only illustrative of the principles of the application. Without departing from the spirit and scope of the application, various changes and improvements can be made to the application, and these changes and improvements all fall within the scope of the claimed application. The scope of protection of the application is defined by the appended claims and their equivalents.

Claims

1. A raw material gas condensing separation device with cold recovery, characterized by, The application relates to a low-temperature gas purification device, which comprises a shell (1) in a barrel shape with an arc-shaped bottom surface, a low-temperature liquid inlet and outlet (18) arranged at the center of the bottom of the shell (1), an upper cover arranged at the top of the shell (1), a gas discharge port (17) arranged at the center of the upper cover, a low-temperature gas inlet (1601) arranged on the upper cover of the shell (1), a low-pressure regulating valve (2), a low-temperature gas outlet (1404), a raw gas inlet (1301), a normal-temperature ultrapure gas outlet (1306), a low-temperature ultrapure gas inlet (1305), a low-temperature pure gas outlet (1304) and a high-pressure regulating valve (10). The low-temperature gas inlet (1601) is connected with the low-temperature gas outlet (1602) through a pipeline, and the low-temperature gas outlet (1602) is arranged in the middle of the shell. The outlet of the low-pressure regulating valve (2) is connected with the low-pressure regulating valve outlet (1502) at the bottom of the shell through a pipeline, and the inlet is connected with the low-pressure separator liquid outlet (1501); the low-pressure separator liquid outlet (1501) is arranged at the bottom of the low-pressure separator (6), the low-pressure separator (6) is further provided with a low-pressure separator liquid inlet (1402) and is connected with the high-pressure regulating valve (10) through a pipeline, and the low-pressure separator (6) is provided with a low-pressure separator gas outlet (1403) at the top end and is connected with the low-temperature gas outlet (1404) through a pipeline. The raw gas inlet (1301) is connected with the upper distributor (12) at the lower end, the upper distributor (12) is provided with an upper collector (11) at the lower end, the upper collector (11) is connected with the normal-temperature ultrapure gas outlet (1306) through a pipeline, the upper collector (11) is provided with a coiled tube type condensation heat exchanger (3) at the lower end, and the lower end of the coiled tube type condensation heat exchanger (3) is provided with a lower distributor (4) and is connected with the low-temperature ultrapure gas inlet (1305) through a pipeline; the lower distributor (4) is provided with a lower collector (5) at the lower end, and the lower collector (5) is connected with the cooling coil (8) through a pipeline. The low-temperature pure gas outlet (1304) is connected with the high-pressure separator low-temperature pure gas outlet (1303) through a pipeline, the low-temperature pure gas outlet (1304) is arranged on the high-pressure separator (7), the high-pressure separator (7) is further provided with a high-pressure separator inlet (1302) in the middle and is connected with the cooling coil (8), and the high-pressure separator (7) is provided with a high-pressure separator liquid outlet (1401) at the bottom and is connected with the high-pressure regulating valve (10) through a pipeline.

2. A raw gas condensing separator with cold recovery according to claim 1, characterized in that, The cylinder and the lower head of the shell (1) are in a Dewar structure with multiple layers of vacuum insulation or vacuum powder insulation or are single-layer outer shells with external insulation; the upper cover is a flat cover connected through flanges or is an oval or butterfly type head.

3. The raw gas condensing separator with cold recovery according to claim 1, characterized in that, The low-pressure regulating valve (2) and the high-pressure regulating valve (10) are fixed on the upper cover, the valve bodies are arranged in the shell (1), and the actuators are arranged outside the shell (1).

4. The raw gas condensing separator with cold recovery according to claim 1, characterized in that, The coiled tube type condensation heat exchanger (3) is a jacketed coiled tube heat exchanger or a heat exchanger in a multi-tube parallel coiled type.

5. The raw gas condensing separator with cold recovery according to claim 1, characterized in that, The low-pressure separator (6) and the high-pressure separator (7) are arranged at the lower part of the coiled tube type condensation heat exchanger (3) and are immersed in low-temperature liquid, and the low-temperature liquid is liquid nitrogen, liquid argon, liquid air, liquid neon or liquid helium medium.

6. The raw gas condensing separator with cold recovery according to claim 1, characterized in that, The lower distributor (4), lower collector (5), upper collector (11), and upper distributor (12) are circular ring-shaped, arc-shaped, or cylindrical pipes.

7. The raw gas condensing separator with cold recovery according to claim 1, characterized in that, The cooling coil (8) is wound outside the low-pressure separator (6) and the high-pressure separator (7) and is immersed in a low-temperature liquid, which is liquid nitrogen, liquid argon, liquid air, liquid neon, or liquid helium medium.

8. A method of using a raw gas condensing separation device with cold recovery according to any one of claims 1-7, characterized in that, The method comprises the following steps: S1, the liquid level of the low-temperature liquid in the device is controlled to completely immerse the low-pressure separator (6) and the high-pressure separator (7), but does not exceed the lower distributor (4), and the operating temperature of the low-temperature liquid is -145℃ to -243℃; S2, the raw gas enters the upper distributor (12) from a raw gas inlet (1301), then enters the coiled pipe condenser (3) and is cooled to -145℃ to -243℃ to obtain a gas-liquid mixture, and then enters the lower collector (5) to be collected, is cooled to the temperature of the low-temperature liquid by the cooling coil (8), enters the high-pressure separator (7) to be separated into gas and liquid, and the gas phase is discharged through a low-temperature pure gas outlet (1304); S3, the liquid phase of the high-pressure separator (7) is throttled to 0.3 to 0.5 MPa by the high-pressure regulating valve (10) and then enters the low-pressure separator (6) to be separated into gas and liquid, the gas phase is discharged from the device to a recovery system, and the liquid phase is throttled to the operating pressure of the low-temperature liquid in the device by the low-pressure regulating valve (2) and is discharged to the bottom of the device to supplement the consumption of the low-temperature liquid; S4, the ultra-pure gas enters the coiled pipe condenser (3) after being distributed by the lower distributor (5) through a low-temperature ultra-pure gas inlet (1305) to provide cold energy for the coiled pipe condenser (3), and the low-temperature ultra-pure gas is reheated and enters the upper collector (11) and is discharged from a normal-temperature ultra-pure gas outlet (1306); S5, the low-temperature gas entering through a low-temperature gas inlet (1601) is mixed with the low-temperature liquid evaporation gas and passes through the gap between the outer shell and the coiled pipe of the coiled pipe condenser (3) to provide cold energy for the coiled pipe condenser (3), and the low-temperature gas is reheated and discharged from a gas discharge port (17).

9. The method of claim 8, wherein the method further comprises: The operating pressure of the raw gas is 2 to 20 MPa, the nitrogen and oxygen impurity content is 20 to 95%, and the temperature is normal temperature.

10. The method of claim 8, wherein the feed gas condensing and separating apparatus with cold recovery is characterized in that, The gas phase purity of the high-pressure separator (7) is 90 to 99.5%.

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