CN219494594U - Cold volume full recovery unit of air separation plant argon system - Google Patents

Cold volume full recovery unit of air separation plant argon system Download PDF

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Publication number
CN219494594U
CN219494594U CN202320482373.1U CN202320482373U CN219494594U CN 219494594 U CN219494594 U CN 219494594U CN 202320482373 U CN202320482373 U CN 202320482373U CN 219494594 U CN219494594 U CN 219494594U
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CN
China
Prior art keywords
pipeline
argon
heat exchanger
air separation
tower
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Active
Application number
CN202320482373.1U
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Chinese (zh)
Inventor
王杰杰
关磊
刘航
柴育鹏
陈龙
袁丙栋
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Lianyungang Petrochemical Co Ltd
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Lianyungang Petrochemical Co Ltd
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Priority to CN202320482373.1U priority Critical patent/CN219494594U/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • F25J3/048—Argon recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The utility model relates to the field of air separation devices, in particular to a full cold recovery device of an argon system of an air separation device, which comprises a heat exchanger, a main tower, a crude argon tower and a fine argon tower, wherein the rear part of the crude argon tower is connected with a vent pipeline, the vent pipeline is connected with a bypass pipeline, the bypass pipeline is connected with the heat exchanger, and a vent valve group is arranged on a pipe body of the bypass pipeline between the heat exchanger and the vent pipeline: through the full recovery of argon system cold energy, the yield of liquid oxygen and liquid nitrogen is greatly improved, and the operation energy consumption of the device is reduced on the basis of ensuring the stable operation of the device.

Description

Cold volume full recovery unit of air separation plant argon system
Technical Field
The utility model relates to the field of air separation devices, in particular to a full cold energy recovery device of an argon system of an air separation device.
Background
The air separation device is a set of industrial equipment device for separating each component gas in the air and respectively producing oxygen, nitrogen, argon and other gases of the air components. At present, in the technical process of an argon system of an air separation device, an emptying pipeline is arranged behind a crude argon tower, two emptying valves are connected to the emptying pipeline, and the emptying pipeline is mainly used for emptying the crane, normally operating and treating nitrogen racing and emptying the crane when the argon system is stopped so as to ensure the stable operation of the whole air separation device and the extraction rate of oxygen.
In the prior art, under the condition that the air separation device runs under low load or the capacity needs to be reduced, liquid argon products cannot be produced, and only an emptying pipeline of argon behind a crude argon tower can be emptied, and because the emptying pipeline is low-temperature gas, the temperature is about-180 ℃, the direct discharge causes huge waste of energy consumption, and meanwhile, the production of liquid oxygen and liquid nitrogen is limited.
Disclosure of Invention
The utility model aims to provide a full cold energy recovery device of an argon system of an air separation device, which has the characteristics of fully recovering cold energy of argon gas emptying and increasing the product yield of liquid oxygen and liquid nitrogen through the recovered cold energy of the argon gas.
The technical aim of the utility model is realized by the following technical scheme: the utility model provides a full recovery unit of cold energy of air separation unit argon system, includes heat exchanger, main tower, crude argon tower, smart argon tower, connects the blow off line behind the crude argon tower, is connected with bypass pipeline on the blow off line, and bypass pipeline is connected with the heat exchanger, is provided with the blow off valves on the body of pipe that bypass pipeline is located between heat exchanger and the blow off pipeline.
Through adopting above-mentioned technical scheme, in order to satisfy the needs that device argon system driven and daily operating mode handled, set up two blow-down valves behind crude argon tower for go out the blowdown of crude argon tower argon gas, because this blowdown air is low-temperature gas, the temperature is about-180 ℃, in order to retrieve this partial cold volume, increased the bypass line between two blow-down valves, install the blow-down valves on the bypass line, will go out crude argon tower argon gas and cause the crude argon passageway of heat exchanger to carry out cold volume recovery through the blow-down valves, thereby reach the purpose that cold volume was whole to retrieve.
Preferably, the vent valve set includes a first vent valve and a second vent valve.
By adopting the technical scheme, when the bypass pipeline is not put into use, the first emptying valve and the second emptying valve are closed, so that the tightness of the bypass pipeline is ensured.
Preferably, a pressure release pipeline is connected to a bypass pipeline between the first relief valve and the second relief valve, and the pressure release pipeline is provided with a pressure release valve.
By adopting the technical scheme, when the pressure in the bypass pipeline is overlarge, the pressure in the pipeline can be released by opening the pressure release valve.
Preferably, a heating pipeline is connected to a bypass pipeline between the first vent valve and the second vent valve, and a heating valve is connected to the heating pipeline.
By adopting the technical scheme, the temperature of the discharged gas is as low as-180 ℃, so that the discharge valve group is easily iced, and external air enters a bypass pipeline to circulate by opening the heating valve and the pressure release valve to contact with the first discharge valve and the second discharge valve for heating.
Preferably, a dirty nitrogen pipe is connected between the heat exchanger and the main tower, a bypass pipeline is positioned between the emptying valve group and the heat exchanger, a branch pipeline is connected on the pipe body, the branch pipeline is connected with the dirty nitrogen pipe, and a dirty nitrogen valve is arranged on the branch pipeline.
Through adopting above-mentioned technical scheme, when the difference will be through bypass line and the empty valves of blowing out, close the valve of blowing out, open dirty nitrogen valve, make bypass line and dirty nitrogen pipe connection, utilize bypass line to carry dirty nitrogen, because bypass line connects the heat exchanger, also can carry out heat transfer to dirty nitrogen when so bypass line carries dirty nitrogen.
In summary, the utility model has the following beneficial effects: a bypass pipeline is additionally arranged between the two vent valves, the vent valve group is arranged on the bypass pipeline, the crude argon channel of the heat exchanger is caused to conduct cold energy recovery through the crude argon tower argon gas, the purpose of total cold energy recovery is achieved, and the product yield of liquid oxygen and liquid nitrogen is increased through the recovered argon cold energy.
Drawings
FIG. 1 is a schematic diagram of the structure of a split device argon system in an embodiment;
fig. 2 is an enlarged schematic view of the portion a in fig. 1.
In the figure, 1, a heat exchanger; 11. a main tower; 12. a crude argon column; 13. a refined argon tower; 14. a vent line; 2. a bypass line; 21. a vent valve group; 22. a first vent valve; 23. a second vent valve; 3. a pressure release line; 31. a pressure release valve; 4. a warming pipeline; 41. a warming valve; 5. a dirty nitrogen pipe; 51. a branch line; 52. a dirty nitrogen valve.
Detailed Description
The present utility model will be described in further detail with reference to the accompanying drawings.
The present embodiment is only for explanation of the present utility model and is not to be construed as limiting the present utility model, and modifications to the present embodiment, which may not creatively contribute to the present utility model as required by those skilled in the art after reading the present specification, are all protected by patent laws within the scope of claims of the present utility model.
Examples: the utility model provides a cold energy full recovery unit of air separation plant argon system, as shown in fig. 1 and fig. 2, includes heat exchanger 1, main tower 11, crude argon tower 12, smart argon tower 13, connects through the pipeline between four. The direction of fluid transport within the conduit is indicated by the arrow.
The emptying pipeline 14 is connected behind the crude argon tower 12, the bypass pipeline 2 is connected to the emptying pipeline 14, the bypass pipeline 2 is connected with the heat exchanger 1, the emptying valve group 21 is installed on the pipe body of the bypass pipeline 2 between the heat exchanger 1 and the emptying pipeline 14, and the emptying valve group 21 comprises a first emptying valve 22 and a second emptying valve 23 which are installed in series. The bypass pipeline 2 between the first relief valve 22 and the second relief valve 23 is connected with a pressure release pipeline 3 and a heating pipeline 4, the pressure release pipeline 3 is provided with a pressure release valve 31, and the heating pipeline 4 is provided with a heating valve 41.
A dirty nitrogen pipe 5 is connected between the heat exchanger 1 and the main tower 11, a branch pipe 51 is connected on the pipe body of the bypass pipeline 2 between the emptying valve group 21 and the heat exchanger 1, the branch pipe 51 is connected with a branch of the dirty nitrogen pipe 5, and a dirty nitrogen valve 52 is arranged on the branch pipe 51.
The using method comprises the following steps: under the normal working state of the argon system, air from the previous working procedure enters the main tower 11 after heat exchange by the heat exchanger 1, the air is rectified in the main tower 11, liquid oxygen and liquid nitrogen products are obtained by rectifying the air in the main tower 11, meanwhile, coarse argon is extracted from the upper part of the main tower 11 and enters the coarse argon tower 12, the coarse argon enters the refined argon tower 13 after the tower is rectified, and a refined liquid argon product is obtained from the bottom of the refined argon tower 13 and enters the liquid argon storage tank.
In the start-up stage of the air separation device, the rectifying device needs to be continuously cooled to about-180 ℃, and in order to ensure the cooling effect of an argon system, the current process flow is to directly empty a large amount of low-temperature gas so as to keep the flow of the argon system, and the aim of cooling is achieved, but a large amount of cold energy is wasted. In the present embodiment, by opening the vent valve group 21 and incorporating this partially vented gas into the heat exchanger 1 to recover the cold of the vented gas, the time to start can be shortened.
When the argon system is cooled to the target temperature and the effusion purification stage is started gradually, the vent valve group 21 is closed gradually, and the dirty nitrogen valve 52 is opened. In normal operation, the vent valve block 21 is in a closed state and the dirty nitrogen valve 52 is in a fully open configuration to ensure proper operation of the argon passage of the heat exchanger 1.
In normal operation, to ensure tightness of the closing of the vent valve set 21, prevent the dirty nitrogen from reversely flowing to the argon system through the dirty nitrogen valve 52, and cause pollution of argon purity, if the vent valve set 21 is not tightly closed, it is considered that the intermediate pressure release valve 31 and the warming valve 41 are opened while the vent valve set 21 is closed, so as to ensure that the gases do not cross each other.
When the argon system is used in the exit stage, the refined argon tower 13 needs to be stopped, and the crude argon tower 12 needs to ensure the stable operation of the rectification of the air separation device and the extraction rate of oxygen, so that the normal operation is ensured, and the current process flow is that the gas of the crude argon tower 12 is directly discharged, under the working condition, the liquid argon product cannot be obtained, and the pressurized liquid oxygen and liquid nitrogen product cannot be obtained, because part of cold energy is wasted. In this embodiment, when the refined argon column 13 exits, the gas exiting the crude argon column 12 may enter the heat exchanger 1 through the vent valve group 21, so as to recover the cold energy of the gas exiting the crude argon column 12, and the cold energy may be converted into liquid oxygen and liquid nitrogen products, so that the yields of liquid oxygen and liquid nitrogen are greatly improved.
In the process of opening the vent valve group 21, the dirty nitrogen valve 52 needs to be closed, and meanwhile, attention needs to be paid to the fact that the argon channel of the heat exchanger 1 cannot generate negative pressure, and the pipeline is blocked by freezing.
After the technical scheme of the embodiment is put into use, the expected use effect is achieved. Specific data before and after use are as follows:
liquid product yield before use of the present technical proposal
Name of the name Yield (Nm) 3 /h) Purity of
Liquid oxygen 300 ≤1ppmO 2 ，≤2ppmN 2 ，
Liquid nitrogen 100 ≥99.8％O 2
Liquid argon 1250 ≤3ppmO 2
Liquid product yield after using the technical proposal
Name of the name Yield (Nm) 3 /h) Purity of
Liquid oxygen 300-1200 ≤1ppmO 2 ，≤2ppmN 2 ，
Liquid nitrogen 100-1200 ≥99.8％O 2
Liquid argon 0-1250 ≤3ppmO 2
Through actual production inspection, when the argon system operates normally, liquid oxygen, liquid nitrogen and liquid argon products can reach initial design values, after the argon system refined argon tower exits, the yield of liquid oxygen and liquid nitrogen is greatly improved through full recovery of the cold energy of the argon system, and the operation energy consumption of the device is reduced on the basis of ensuring the stable operation of the device.

Claims (5)

1. The utility model provides a full recovery unit of cold energy of air separation plant argon system, includes heat exchanger (1), main tower (11), crude argon tower (12), smart argon tower (13), and its characterized in that connects blow-down pipeline (14) behind crude argon tower (12), is connected with bypass pipeline (2) on blow-down pipeline (14), and bypass pipeline (2) are connected with heat exchanger (1), are provided with blow-down valves (21) on the pipe shaft that bypass pipeline (2) are located between heat exchanger (1) and blow-down pipeline (14).
2. The full cold recovery device of an argon system of an air separation plant according to claim 1, wherein the vent valve group (21) comprises a first vent valve (22) and a second vent valve (23).
3. The full cold recovery device of an argon system of an air separation device according to claim 2, wherein a pressure release pipeline (3) is connected to a bypass pipeline (2) between the first vent valve (22) and the second vent valve (23), and a pressure release valve (31) is arranged on the pressure release pipeline (3).
4. A full cold recovery device for an argon system of an air separation device according to claim 3, wherein a heating pipeline (4) is connected to a bypass pipeline (2) between the first vent valve (22) and the second vent valve (23), and a heating valve (41) is connected to the heating pipeline (4).
5. The full cold recovery device of an argon system of an air separation device according to claim 1, wherein a dirty nitrogen pipe (5) is connected between the heat exchanger (1) and the main tower (11), a branch pipe line (51) is connected on a pipe body of the bypass pipeline (2) between the vent valve group (21) and the heat exchanger (1), the branch pipe line (51) is connected with the dirty nitrogen pipe (5), and a dirty nitrogen valve (52) is arranged on the branch pipe line (51).
CN202320482373.1U 2023-03-14 2023-03-14 Cold volume full recovery unit of air separation plant argon system Active CN219494594U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202320482373.1U CN219494594U (en) 2023-03-14 2023-03-14 Cold volume full recovery unit of air separation plant argon system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202320482373.1U CN219494594U (en) 2023-03-14 2023-03-14 Cold volume full recovery unit of air separation plant argon system

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Publication Number Publication Date
CN219494594U true CN219494594U (en) 2023-08-08

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