Pipe infusion argon cold energy recovery method and device

Abstract

The invention discloses a pipe infusion argon cold energy recovery device and method, and relates to the technical field of liquid argon cold energy recovery. The device comprises a circulating nitrogen pressure unit, a cold energy recovery cold box and a liquid argon pump, wherein the cold energy recovery cold box comprises a main heat exchanger, a subcooler and a liquefied plate heat exchanger. The main heat exchanger is provided with four inlets and outlets, and the subcooler and the liquefying plate heat exchanger are each provided with two inlets and outlets. Medium-pressure nitrogen is pressurized by a circulating nitrogen pressure unit, then enters a main heat exchanger to be cooled and liquefied and then is supercooled by a cooler, part of liquid nitrogen returns to the supercooler to serve as a cold source, part of liquid nitrogen enters an inlet of a liquid nitrogen storage tank, and the rest liquid nitrogen is emptied after being reheated; liquid argon is pressurized by the liquid argon pump, enters the main heat exchanger for vaporization and reheating, and is output to an argon pipe network; oxygen is liquefied by the liquefying plate heat exchanger and then enters an inlet of the liquid oxygen storage tank. The circulating nitrogen compressor adopts a piston type compressor, and a pipeline is laid outdoors in an overhead mode. Liquid nitrogen and liquid oxygen are produced through liquid argon cold energy recovery, efficient utilization of cold energy is achieved, energy consumption is reduced, no waste gas or waste water is discharged in the technological process, and operation is safe and reliable.

Description

Technical Field

[0001] The present invention belongs to the technical field of cryogenic energy recovery of liquid argon, and relates to a method and device for recovering cryogenic energy of pipeline-transported liquid argon. Background Art

[0002] Liquid argon, as a colorless, odorless, and non-flammable inert gas, is in a liquid state under normal temperature and pressure. Due to its chemical stability and excellent heat conduction performance, it has a wide range of applications in multiple industrial fields. In semiconductor manufacturing, liquid argon is commonly used in the cooling process to ensure the processing quality of precision components; in the metal processing field, liquid argon is used as a protective atmosphere, especially in the welding processes of special metals such as aluminum, magnesium, copper and their alloys, and stainless steel, effectively preventing material oxidation or nitridation; in the aerospace, shipbuilding, atomic energy industry, and machinery manufacturing, argon gas has become an ideal protective gas due to its non-combustible and non-supporting combustion characteristics. In addition, liquid argon also has important applications in the medical field (such as cryotherapy) and scientific research (such as low-temperature experiments).

[0003] The vaporization process of liquid argon is a key step in converting liquid argon into gaseous argon to meet industrial needs. However, traditional liquid argon vaporization methods have significant limitations. Currently, air-cooled vaporizers are commonly used equipment, which vaporize liquid argon through the heat of ambient air. However, this method is inefficient in low-temperature environments and is prone to a large amount of icing, increasing equipment maintenance costs and posing a fall risk in the surrounding area. Another common method is to use steam or electric heating vaporizers, but this requires a large amount of energy consumption, especially in the context of high energy prices, resulting in high operating costs. More importantly, the cryogenic energy (latent heat and sensible heat) released during the liquid argon vaporization process is usually wasted and not effectively recovered and utilized, resulting in low energy utilization efficiency.

[0004] In recent years, cryogenic energy recovery technology has gradually received attention, and some industrial systems have tried to transfer the cryogenic energy of liquid argon vaporization to other media, such as liquefied nitrogen or oxygen, through heat exchangers. However, existing cryogenic energy recovery technologies have the following deficiencies: First, the design of the recovery system is complex and the integration degree is low, making it difficult to handle the liquefaction requirements of multiple gases simultaneously; second, the cryogenic energy utilization rate is limited, and some cold energy is still dissipated in the form of waste heat; third, there is a lack of special recovery devices for pipeline-transported liquid argon, resulting in insignificant economic benefits of cryogenic energy recovery. For example, some recovery systems can only use cryogenic energy for the liquefaction of a single gas and fail to fully utilize the potential of liquid argon cryogenic energy; in addition, existing devices have insufficient considerations in the design and safety of low-temperature pipelines, restricting their popularization and application in industrial environments.

[0005] In view of this, it is particularly necessary to develop an efficient and comprehensive method and device for recovering cryogenic energy of pipeline-transported liquid argon. Summary of the Invention

[0006] In view of this, the purpose of the present invention is to solve the problem of cold energy recovery and utilization of liquid argon vaporization, and a method and device for recovering cold energy from pipeline-transported liquid argon are provided.

[0007] To achieve the above object, the present invention provides the following technical solutions:

[0008] A device for recovering cold energy from pipeline-transported liquid argon includes a circulating nitrogen compressor unit, a cold energy recovery cold box, and a liquid argon pump; the cold energy recovery cold box includes a main heat exchanger, a subcooler, and a liquefaction plate heat exchanger;

[0009] The main heat exchanger is provided with four groups of inlets and outlets, namely a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet, a second heat exchange outlet, a third heat exchange inlet, a third heat exchange outlet, a fourth heat exchange inlet, and a fourth heat exchange outlet; the subcooler is provided with two groups of inlets and outlets, namely a first subcooling inlet, a first subcooling outlet, a second subcooling inlet, and a second subcooling outlet; the liquefaction plate heat exchanger is provided with two groups of inlets and outlets, namely a first liquefaction inlet, a first liquefaction outlet, a second liquefaction inlet, and a second liquefaction outlet;

[0010] The medium-pressure nitrogen pipeline is connected from the medium-pressure nitrogen main pipe in the factory area and is communicated with the inlet of the circulating nitrogen compressor. The outlet of the circulating nitrogen compressor is communicated with the first heat exchange inlet. The first heat exchange outlet is throttled by throttle valve V1 and then divided into two paths. One path is communicated with the second heat exchange inlet, and the other path is communicated with the first subcooling inlet. The second heat exchange outlet is communicated with the inlet of the circulating nitrogen compressor; the first subcooling outlet is divided into three paths. One path is throttled by throttle valve V3 and then communicated with the second subcooling inlet. Another path is throttled by throttle valve V2 and then communicated with the inlet of the liquid nitrogen storage tank. The last path is throttled by throttle valve V4 and then communicated with the second liquefaction inlet; the second subcooling outlet is communicated with the third heat exchange inlet, and the third heat exchange outlet is communicated with the low-pressure nitrogen pipeline network; the second liquefaction outlet is communicated with the atmosphere, and the normal-pressure nitrogen is discharged to the atmosphere; the first liquefaction inlet is communicated with the oxygen pipeline network in the factory area, and the first liquefaction outlet is throttled by throttle valve V5 and then communicated with the inlet of the liquid oxygen storage tank;

[0011] The inlet of the liquid argon pump is communicated with the liquid argon storage tank, and the outlet of the liquid argon pump is communicated with the fourth heat exchange inlet. The fourth heat exchange outlet is communicated with the argon pipeline network.

[0012] Further, the circulating nitrogen compressor adopts a piston compressor.

[0013] A method for recovering cold energy from pipeline-transported liquid argon uses the device for recovering cold energy from pipeline-transported liquid argon as described above. The nitrogen from the nitrogen pipeline network in the factory area is pressurized by the circulating nitrogen compressor unit and then enters the main heat exchanger in the cold energy recovery cold box. After being cooled and liquefied, it enters the subcooler for subcooling; the liquid argon from the liquid argon storage tank after being pressurized by the liquid argon pump enters the main heat exchanger in the cold energy recovery cold box, is vaporized and reheated, and then enters the argon pipeline network in the factory area;

[0014] The subcooled liquid nitrogen has three destinations. A part of the subcooled liquid nitrogen is throttled to 0.03 MPa and then returned to the subcooler as a cold source. After vaporizing and reheating, it enters the main heat exchanger and continues to be reheated to room temperature. The reheated low-pressure nitrogen is returned to the nitrogen pipeline network. Another part is throttled to 0.06 MPa and enters the liquid nitrogen storage tank. The remaining liquid nitrogen is throttled to 0.02 MPa, reheated through the liquefaction plate heat exchanger, and then vented.

[0015] After the oxygen is liquefied by the liquefaction plate heat exchanger, it is throttled to 0.01 MPa by a throttle valve and then enters the liquid oxygen storage tank.

[0016] Furthermore, the nitrogen from the nitrogen pipeline network in the plant area has a pressure of 0.63 MPa. The nitrogen is pressurized to 5.1 MPa by the circulating nitrogen compressor unit and then enters the main heat exchanger in the cold energy recovery cold box.

[0017] Furthermore, for vaporizing the liquid argon at 0.05 MPa, the corresponding heat source argon is raised to 1.985 MPa.

[0018] Furthermore, for liquefying the oxygen at 0.1 MPa, the corresponding liquid oxygen pressure is 0.01 MPa.

[0019] Furthermore, the gas pipelines and cryogenic liquid pipelines are laid overhead outdoors.

[0020] The beneficial effects of the present invention are as follows:

[0021] The tube-injected liquid argon cold energy recovery device and method of the present invention achieve the efficient recovery and comprehensive utilization of the cold energy of liquid argon vaporization through innovative design, demonstrating significant advantages in many aspects.

[0022] First of all, the present invention significantly improves the energy utilization efficiency. Through the main heat exchanger, subcooler, and liquefaction plate heat exchanger in the cold energy recovery cold box, the cold energy released by the vaporization of liquid argon is effectively transferred to the liquefaction processes of nitrogen and oxygen, replacing the high-energy consumption methods of traditional steam or electric heating vaporizers. This design of cold energy recycling greatly reduces the external energy demand and provides an energy-saving solution for industrial gas treatment.

[0023] Secondly, the present invention produces high-value-added liquid nitrogen and liquid oxygen products by liquefying the surplus nitrogen and oxygen in the plant area. These products can be widely used in industrial, medical, and scientific research fields and have high market value. Compared with the waste of cold energy after the traditional vaporization of liquid argon, the present invention converts the cold energy into salable liquid products, significantly enhancing the economic benefits.

[0024] In addition, the present invention realizes environmental friendliness during operation. The argon gas after the vaporization of liquid argon directly enters the pipe network. Part of the liquid nitrogen returns to the nitrogen pipe network after reheating, and the remaining nitrogen is discharged at atmospheric pressure. There is no emission of waste gas, waste water or dust during the whole process. Compared with the traditional air-cooled vaporizer, the present invention avoids the equipment corrosion and environmental impact caused by icing, meeting the requirements of green production.

[0025] In terms of safety, the present invention eliminates the risks of slippery ground and falling caused by icing of the traditional air-cooled vaporizer through the closed cold energy recovery cold box. The outdoor gas and cryogenic liquid pipelines are laid overhead, further reducing the leakage risk and enhancing the reliability of the device operation.

[0026] Finally, the device of the present invention has a high degree of integration and strong adaptability. The circulating nitrogen compressor unit adopts a piston compressor with variable frequency control, which can flexibly adapt to the requirements of different working conditions. The compact system design makes it applicable to industrial gas pipe networks of various scales, providing convenience for the popularization and application of liquid argon cold energy recovery.

[0027] Other advantages, objectives and features of the present invention will be described to some extent in the subsequent specification, and to some extent, will be obvious to those skilled in the art based on the study of the following text, or can be taught from the practice of the present invention. The objectives and other advantages of the present invention can be realized and obtained through the following specification. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] In order to make the objectives, technical solutions and advantages of the present invention clearer, the present invention will be described in detail preferably with reference to the accompanying drawings, where:

[0029] Figure 1 is the schematic diagram of the device for recovering cold energy from pipeline-transported liquid argon in the present invention.

[0030] Reference numerals: 1 - circulating nitrogen compressor; 2 - main heat exchanger; 3 - subcooler; 4 - liquefaction plate heat exchanger; 5 - liquid argon pump; 6 - liquid nitrogen storage tank; 7 - liquid oxygen storage tank; 21 - first heat exchange inlet; 25 - first heat exchange outlet; 26 - second heat exchange inlet; 22 - second heat exchange outlet; 27 - third heat exchange inlet; 23 - third heat exchange outlet; 28 - fourth heat exchange inlet; 24 - fourth heat exchange outlet; 31 - first subcooling inlet; 33 - first subcooling outlet; 34 - second subcooling inlet; 32 - second subcooling outlet; 41 - first liquefaction inlet; 43 - first liquefaction outlet; 44 - second liquefaction inlet; 42 - second liquefaction outlet; 51 - liquid argon pump inlet; 52 - liquid argon pump outlet; 61 - liquid nitrogen storage tank inlet; 71 - liquid oxygen storage tank inlet. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0031] The following describes the embodiments of the present invention through specific examples. Those skilled in the art can easily understand other advantages and effects of the present invention from the content disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments. Various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention. It should be noted that the drawings provided in the following embodiments only illustrate the basic concept of the present invention in a schematic manner. Without conflict, the following embodiments and the features in the embodiments can be combined with each other.

[0032] Among them, the drawings are only for illustrative purposes, showing only schematic diagrams, not physical diagrams, and should not be construed as a limitation to the present invention; in order to better illustrate the embodiments of the present invention, some components in the drawings will be omitted, enlarged or reduced, which does not represent the size of the actual product; for those skilled in the art, it is understandable that some well-known structures and their descriptions in the drawings may be omitted.

[0033] In the drawings of the embodiments of the present invention, the same or similar reference numerals correspond to the same or similar components; in the description of the present invention, it should be understood that if there are terms such as "upper", "lower", "left", "right", "front", "rear", etc. indicating the orientation or positional relationship, they are based on the orientation or positional relationship shown in the drawings. It is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation. Therefore, the terms describing the positional relationship in the drawings are only for illustrative purposes and should not be construed as a limitation to the present invention. For those of ordinary skill in the art, the specific meanings of the above terms can be understood according to specific circumstances.

[0034] Embodiment 1

[0035] Please refer to Figure 1 , which is a tube infusion argon cold energy recovery device, including a circulating nitrogen compressor unit, a cold energy recovery cold box, and a liquid argon pump; the cold energy recovery cold box is designed in three sections. One section recovers sensible heat and latent heat, one section is used for subcooling, and one section is used for liquefaction. It includes a main heat exchanger 2, a subcooler 3, a liquefaction plate heat exchanger 4, a liquid argon pump 5, a liquid nitrogen storage tank 6, and a liquid oxygen storage tank 7; the main heat exchanger 2 is provided with four groups of inlets and outlets, namely a heat exchange first inlet 21, a heat exchange first outlet 25, a heat exchange second inlet 26, a heat exchange second outlet 22, a heat exchange third inlet 27, a heat exchange third outlet 23, a heat exchange fourth inlet 28, and a heat exchange fourth outlet 24; the subcooler 3 is provided with two groups of inlets and outlets, namely a subcooling first inlet 31, a subcooling first outlet 33, a subcooling second inlet 34, and a subcooling second outlet 32; the liquefaction plate heat exchanger is provided with two groups of inlets and outlets, namely a liquefaction first inlet 41, a liquefaction first outlet 43, a liquefaction second inlet 44, and a liquefaction second outlet 42;

[0036] The medium-pressure nitrogen pipeline is connected to the medium-pressure nitrogen main pipe in the plant area and is connected to the inlet 11 of the circulating nitrogen compressor. The outlet 12 of the circulating nitrogen compressor is connected to the first heat exchange inlet 21. After the first heat exchange outlet 25 is throttled by the throttle valve V1, it is divided into two paths. One path is connected to the second heat exchange inlet 26, and the other path is connected to the first subcooling inlet 31. The second heat exchange outlet 22 is connected to the inlet 11 of the circulating nitrogen compressor; the first subcooling outlet 33 is divided into three paths. One path is throttled by the throttle valve V3 and then connected to the second subcooling inlet 34. Another path is throttled by the throttle valve V2 and then connected to the inlet 61 of the liquid nitrogen storage tank. The last path is throttled by the throttle valve V4 and then connected to the second liquefaction inlet 44; the second subcooling outlet 32 is connected to the third heat exchange inlet 27, and the third heat exchange outlet is connected to the low-pressure nitrogen pipeline network; the second liquefaction outlet 42 is connected to the atmosphere, and the normal-pressure nitrogen is discharged to the atmosphere; the first liquefaction inlet 41 is connected to the oxygen pipeline network in the plant area, and the first liquefaction outlet 43 is throttled by the throttle valve V5 and then connected to the inlet 71 of the liquid oxygen storage tank;

[0037] The inlet 51 of the liquid argon pump is connected to the liquid argon storage tank, and the outlet 52 of the liquid argon pump is connected to the fourth heat exchange inlet 28. The fourth heat exchange outlet 24 is connected to the argon pipeline network;

[0038] Among them, the circulating nitrogen compressor 1 adopts a piston compressor and uses variable frequency control.

[0039] The outdoor gas pipelines and cryogenic liquid pipelines connected are laid overhead.

[0040] Embodiment 2

[0041] A method for recovering cold energy of pipeline-transported liquid argon uses the pipeline-transported liquid argon cold energy recovery device in Embodiment 1 to vaporize liquid argon at 0.05 MPa, and the corresponding heat source argon gas is raised to 1.985 MPa.

[0042] The nitrogen gas at a pressure of 0.63 MPa from the nitrogen pipeline network in the plant area is pressurized to 5.1 MPa by the circulating nitrogen compressor unit 1 and enters the main heat exchanger 2 in the cold energy recovery cold box. After being cooled and liquefied, it enters the subcooler 3 for subcooling; the liquid argon pressurized by the liquid argon pump 5 from the liquid argon storage tank enters the main heat exchanger 2 in the cold energy recovery cold box. After being vaporized and reheated, it enters the argon pipeline network in the plant area; the oxygen from the oxygen pipeline network in the plant area is liquefied by the liquefaction plate heat exchanger 4 and then enters the liquid oxygen storage tank 7.

[0043] The subcooled liquid nitrogen has three destinations. A part of the subcooled liquid nitrogen is throttled to 0.03 MPa and then returns to the subcooler 3 as a cold source. After being vaporized and reheated, it enters the main heat exchanger 2 again to continue reheating to room temperature, and the reheated low-pressure nitrogen gas returns to the nitrogen pipeline network; another part is throttled to 0.06 MPa and enters the liquid nitrogen storage tank 6; the remaining liquid nitrogen is throttled to 0.02 MPa, reheated by the liquefaction plate heat exchanger 4, and then discharged;

[0044] Among them, the medium-pressure nitrogen pipeline is taken out from the medium-pressure nitrogen main pipe on the secondary oxygen production main pipe gallery and sent to the circulating nitrogen compressor 1, and the handover point pressure is about 0.63 MPa. Liquid argon is taken out from the liquid argon main pipe on the primary oxygen production main pipe gallery and sent to the liquid argon cold energy recovery cold box, and the handover point pressure is about 2 MPa. Oxygen is taken out from the oxygen main pipe on the tertiary oxygen production main pipe gallery and sent to the liquefaction plate heat exchanger 4, and the handover point pressure is 0.1 MPa. Low-pressure nitrogen is vented from the liquefaction plate heat exchanger. Liquid nitrogen is taken out from the liquid argon cold energy recovery cold box and sent to the liquid nitrogen storage tank on the primary oxygen production main pipe gallery, and the handover point pressure is about 0.06 MPa. Liquid oxygen is taken out from the liquefaction plate heat exchanger and sent to the liquid oxygen storage tank, and the handover point pressure is about 0.01 MPa. Argon is taken out from the liquid argon cold energy recovery cold box and sent to the argon pipeline network, and the handover point pressure is 1.985 MPa.

[0045] The raw materials used in the present invention: liquid argon: 1500 Nm 3 / h (converted to gaseous state), 0.05 MPa; nitrogen: 1680 Nm 3 / h, 0.63 MPa; oxygen: 300 Nm 3 / h, 0.1 MPa. The products obtained are: liquid nitrogen: 984 Nm 3 / h (converted to gaseous state), 0.06 MPa; liquid oxygen: 300 Nm 3 / h, 0.01 MPa; argon: 1500 Nm 3 / h, 1.985 MPa.

[0046] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit them. Although the present invention has been described in detail with reference to the preferred embodiments, those of ordinary skill in the art should understand that the technical solutions of the present invention can be modified or equivalently replaced without departing from the spirit and scope of the present technical solution, and they should all be covered by the scope of the claims of the present invention.

Claims

1. A tube infusion argon cold energy recovery device, characterized in that: It includes a circulating nitrogen compressor unit, a cold energy recovery cold box, and a liquid argon pump; the cold energy recovery cold box includes a main heat exchanger, a subcooler, and a liquefaction plate heat exchanger; The main heat exchanger is provided with four groups of inlets and outlets, namely a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet, a second heat exchange outlet, a third heat exchange inlet, a third heat exchange outlet, a fourth heat exchange inlet, and a fourth heat exchange outlet; the subcooler is provided with two groups of inlets and outlets, namely a first subcooling inlet, a first subcooling outlet, a second subcooling inlet, and a second subcooling outlet; the liquefaction plate heat exchanger is provided with two groups of inlets and outlets, namely a first liquefaction inlet, a first liquefaction outlet, a second liquefaction inlet, and a second liquefaction outlet; The medium-pressure nitrogen pipeline is led out from the medium-pressure nitrogen main pipe in the plant area and is connected to the inlet of the circulating nitrogen compressor. The outlet of the circulating nitrogen compressor is connected to the first heat exchange inlet. After being throttled by throttle valve V1, the first heat exchange outlet is divided into two paths. One path is connected to the second heat exchange inlet, and the other path is connected to the first subcooling inlet. The second heat exchange outlet is connected to the inlet of the circulating nitrogen compressor; the first subcooling outlet is divided into three paths. One path is throttled by throttle valve V3 and then connected to the second subcooling inlet. Another path is throttled by throttle valve V2 and then connected to the inlet of the liquid nitrogen storage tank. The last path is throttled by throttle valve V4 and then connected to the second liquefaction inlet; the second subcooling outlet is connected to the third heat exchange inlet, and the third heat exchange outlet is connected to the low-pressure nitrogen pipeline network; the second liquefaction outlet is connected to the atmosphere, and the normal-pressure nitrogen is discharged to the atmosphere; the first liquefaction inlet is connected to the oxygen pipeline network in the plant area, and after being throttled by throttle valve V5, the first liquefaction outlet is connected to the inlet of the liquid oxygen storage tank; The inlet of the liquid argon pump is connected to the liquid argon storage tank, the outlet of the liquid argon pump is connected to the fourth heat exchange inlet, and the fourth heat exchange outlet is connected to the argon pipeline network.

2. The tube infusion argon cold energy recovery device according to claim 1, characterized in that: The circulating nitrogen compressor adopts a piston compressor.

3. A method for recovering argon cold energy in tube infusion, characterized in that: Adopt the tube-type liquid argon cold energy recovery device according to any one of claims 1 to 2. The nitrogen from the nitrogen pipeline network in the plant area is pressurized by the circulating nitrogen compressor unit and then enters the main heat exchanger in the cold energy recovery cold box, is cooled and liquefied, and then enters the subcooler for subcooling; the liquid argon pressurized by the liquid argon pump from the liquid argon storage tank enters the main heat exchanger in the cold energy recovery cold box, is vaporized and reheated, and then enters the argon pipeline network in the plant area; The subcooled liquid nitrogen has three destinations. Part of the subcooled liquid nitrogen is throttled to 0.03 MPa and then returns to the subcooler as a cold source. After being vaporized and reheated, it enters the main heat exchanger again to continue reheating to room temperature, and the reheated low-pressure nitrogen returns to the nitrogen pipeline network; another part is throttled to 0.06 MPa and enters the liquid nitrogen storage tank; the remaining liquid nitrogen is throttled to 0.02 MPa, reheated through the liquefaction plate heat exchanger, and then discharged; After being liquefied by the liquefaction plate heat exchanger, the oxygen is throttled to 0.01 MPa by the throttle valve and then enters the liquid oxygen storage tank.

4. The tube infusion argon cold energy recovery method according to claim 3, characterized in that: The nitrogen from the nitrogen pipeline network in the plant area has a pressure of 0.63 MPa. After being pressurized to 5.1 MPa by the circulating nitrogen compressor unit, the nitrogen enters the main heat exchanger in the cold energy recovery cold box.

5. The tube infusion argon cold energy recovery method according to claim 3, characterized in that: For vaporizing 0.05 MPa of liquid argon, the corresponding heat source argon is raised to 1.985 MPa.

6. The tube infusion argon cold energy recovery method according to claim 3, wherein: For liquefying 0.1 MPa of oxygen, the corresponding liquid oxygen pressure is 0.01 MPa.

7. The tube infusion argon cold energy recovery method according to claim 3, characterized in that: Outdoor gas pipelines and cryogenic liquid pipelines shall be laid overhead.

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