CN215113526U - Dirty nitrogen cooling capacity utilization device in air separation device - Google Patents
Dirty nitrogen cooling capacity utilization device in air separation device Download PDFInfo
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- CN215113526U CN215113526U CN202120942688.0U CN202120942688U CN215113526U CN 215113526 U CN215113526 U CN 215113526U CN 202120942688 U CN202120942688 U CN 202120942688U CN 215113526 U CN215113526 U CN 215113526U
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- 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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
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- 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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
- F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
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- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
- F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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- 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
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
- F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
Abstract
The utility model belongs to a waste nitrogen cooling capacity utilization device in an air separation device; the device comprises a supercharger, a precooling device, a pressure reducing device, a rectifying tower, a heat exchange device and a storage tank which are arranged in an air separation device, wherein a gas phase outlet at the top of the rectifying tower is connected with a gas phase inlet at the lower part of a packed tower through a tube pass of the precooling device; the device has the advantages of simple structure, reasonable design, effective utilization of the waste cold energy in the air separation device, noise pollution reduction, effective reduction of energy consumption in the ammonia synthesis device and improvement of product quality.
Description
Technical Field
The utility model belongs to the technical field of empty dirty nitrogen gas of dividing recycles, concretely relates to dirty nitrogen gas cold volume utilizes device in air separation plant.
Background
When the existing chemical enterprises use the air separation device, the upper tower of the rectifying tower in the air separation device can generate polluted nitrogen with lower temperature, and most enterprises adopt a direct discharge mode because the part of the polluted nitrogen belongs to waste gas; the above-described approach suffers from the following disadvantages: 1. the waste of cold energy is caused; 2. noise pollution is easily generated in the discharging process.
In addition, the reaction gas needs to be cooled for many times in the ammonia synthesis device so as to meet the requirement of normal production; in order to realize multiple cooling, various types of coolers are required to be used for cooling, so that a large amount of energy is consumed, and the cooling effect is poor; directly causes the defect of poor product quality.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a simple structure, reasonable in design, can effectively utilize waste cold volume and noise abatement pollution among the air separation plant, can also effectively reduce the energy consumption among the ammonia synthesizer and improve the dirty nitrogen gas cold volume utilization device among the air separation plant of ware product quality simultaneously.
In order to solve the technical problem, the utility model discloses a realize through following technical scheme:
the utility model provides a dirty nitrogen gas cooling capacity utilizes device among air separation plant, the device includes booster compressor, precooling apparatus, pressure relief device, rectifying column, heat transfer device and the storage tank among the air separation device, the gaseous phase export at rectifying column top links to each other with the gaseous phase import of packed tower lower part through precooling apparatus's tube side, and the upper portion of packed tower is equipped with the circulating water import, and the liquid phase export of packed tower bottom links to each other with the cooling part of circulating compressor in the ammonia synthesis unit and the shell side of circulating water cooler respectively.
Preferably, a gas phase outlet at the top of the packed tower is connected with a vent noise reduction device.
Preferably, a cooling part of a circulating compressor in the ammonia synthesis unit and a shell pass outlet of a circulating water cooler are respectively connected with an inlet of a water cooling tower, and an outlet of the water cooling tower is connected with a circulating water inlet arranged at the upper part of a packed tower through a first centrifugal booster pump; the water cooling tower is communicated with a dosing storage tank with a valve.
Preferably, the liquid phase outlet at the bottom of the packed tower is respectively connected with a cooling part of a circulating compressor in the ammonia synthesis unit and the shell side of a circulating water cooler through a second centrifugal booster pump.
Preferably, the ammonia synthesis unit comprises a circulating compressor, an inlet of the circulating compressor is connected with a feed gas pipeline, and a gas-phase outlet of the circulating compressor is connected with the ammonia storage tank sequentially through a tube pass of the ammonia synthesis device, a tube pass of a circulating water cooler, a reaction gas heat exchange device, a separation device and a tube pass of an ammonia cooler.
Preferably, a gas phase outlet at the top of the reaction gas heat exchange device is connected with a feed gas pipeline.
Preferably, the liquid phase outlet of the separation device is connected with the inlet of the ammonia storage tank.
Preferably, the shell side of the ammonia cooler is connected with a cooling medium heat exchange unit; the cooling medium heat exchange unit comprises a flash evaporation device, a liquid phase outlet of the flash evaporation device is connected with a shell pass inlet of the ammonia cooler, a shell pass outlet of the ammonia cooler is connected with a gas phase inlet of the flash evaporation device, a gas phase inlet of the flash evaporation device is connected with a gas inlet of the cooling medium compressor, and an outlet of the cooling medium compressor is connected with a liquid phase inlet of the flash evaporation device; the mechanical end of the cooling medium compressor is connected with a steam turbine with a steam pipeline.
According to the device for utilizing the cooling capacity of the waste nitrogen in the air separation device, the waste nitrogen can be reused in the air separation device through the gas phase outlet arranged at the top of the rectifying tower and the tube pass of the precooling device, so that the purpose of reducing the cooling capacity consumption of a system in the air separation device is achieved; the waste nitrogen after passing through the pre-cooling device is generally heated to about 8 ℃, and the heated waste nitrogen is in countercurrent contact with circulating water passing through a water cooling tower through a packed tower to exchange heat, so that the circulating water is cooled to about 10 ℃; the arrangement can effectively enhance the cooling effect of the circulating water, and particularly can effectively reduce the energy consumption of the circulating compressor and the cooling effect of the circulating water cooler on the reaction gas by cooling the circulating water in summer, thereby achieving the purpose of reducing the steam usage amount in the cooling medium heat exchange unit; the device has the advantages of simple structure, reasonable design, effective utilization of the waste cold energy in the air separation device, noise pollution reduction, effective reduction of energy consumption in the ammonia synthesis device and improvement of product quality.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described with reference to the accompanying drawings, in which like reference numerals refer to like parts in the drawings. For the sake of simplicity, only the parts related to the utility model are schematically shown in the drawings, and they do not represent the actual structure as a product.
As shown in fig. 1, the utility model relates to a dirty nitrogen cooling volume utilizes device among air separation plant, the device include booster compressor 1, precooling apparatus 2, pressure relief device 3, rectifying column 4, heat transfer device 5 and storage tank 6 among the air separation plant, the gaseous phase export at rectifying column 4 top is passed through precooling apparatus 2's tube side and is linked to each other with gaseous phase import 8 of packed tower 7 lower part, and the upper portion of packed tower 7 is equipped with circulating water import 9, and liquid phase export 10 of packed tower 7 bottom links to each other with the cooling portion of ammonia synthesis unit mesocycle compressor 16 and the shell side of circulating water cooler 18 respectively. The utility model discloses a reform transform based on current air separation plant, dirty nitrogen gas that makes in rectifying column 4 go up the tower carries out the heat transfer through precooling apparatus 2's tube side and feed gas in order to reach the purpose that reduces air separation plant medium system energy resource consumption, simultaneously through adding packed tower 7 in circulating water system, make through circulating water and dirty nitrogen gas countercurrent contact, realize the purpose of effective cooling, and utilize the above-mentioned circulating water after dirty nitrogen gas cooling to get into circulating compressor 16's cooling portion and circulating water cooler 18's shell side respectively, thereby it realizes the purpose that reduces the energy consumption to reach effectively cooling to circulating compressor 16, make the temperature of reaction gas obtain effectual reduction simultaneously, establish the basis for the heat transfer and the separation process in later stage, the reduction of synthetic ammonia system energy consumption has not only been realized, can also effectively improve the quality of ware product.
Further, a gas phase outlet 11 at the top of the packed tower 7 is connected with a vent noise reduction device 31. The utility model discloses used to set up the device of making an uproar 31 of falling of unloading, realized can discharging the purpose under the prerequisite of noise reduction after the heat transfer to the circulating water.
Further, a cooling part of a circulating compressor 16 in the ammonia synthesis unit and a shell pass outlet of a circulating water cooler 18 are respectively connected with an inlet of a water cooling tower 12, and an outlet of the water cooling tower 12 is connected with a circulating water inlet 9 arranged at the upper part of a packed tower 7 through a first centrifugal booster pump 13; the water cooling tower 12 is communicated with a dosing storage tank 14 with a valve. The liquid phase outlet 10 at the bottom of the packed tower 7 is respectively connected with the cooling part of a circulating compressor 16 in the ammonia synthesis unit and the shell side of a circulating water cooler 18 through a second centrifugal booster pump 15. Through the arrangement, the circulating water can be ensured to be fully exchanged with the waste nitrogen in the packed tower 7, and the stable operation of the water cooling tower 12, the circulating compressor 16 and the circulating water cooler 18 is ensured.
Further, the ammonia synthesis unit comprises a circulating compressor 16, an inlet of the circulating compressor 16 is connected with a raw material gas pipeline 23, and a gas-phase outlet of the circulating compressor 16 is connected with an ammonia storage tank 22 through a pipe pass of an ammonia synthesis device 17, a pipe pass of a circulating water cooler 18, a reaction gas heat exchange device 19, a separation device 20 and a pipe pass of an ammonia cooler 21 in sequence. Through the setting and the circulating water after dirty nitrogen heat transfer links to each other with circulating compressor 16's cooling portion and circulating water cooler 18, can realize the characteristics in order to reach the reduction energy consumption to circulating compressor 16's cooling, can also effectively cool down reaction synthetic gas simultaneously, guaranteed that follow-up reaction gas heat transfer device 19 and ammonia cooler 21 reduce energy consumption to and separator 20 is more thorough to gas-liquid separation, guarantee follow-up product quality's characteristics.
Further, a gas phase outlet at the top of the reaction gas heat exchange device 19 is connected with a raw material gas pipeline 23. Through the arrangement, the gas phase in the reaction gas heat exchange device 19 can be recovered and mixed with the raw material gas, so that the temperature of the mixed gas is lower than that of the raw material gas, and the purposes of reducing the energy consumption of the circulating compressor 16 and the cold quantity of a subsequent heat exchange device are achieved.
Further, the liquid phase outlet of the separation device 20 is connected to the inlet of an ammonia storage tank 22.
Further, the shell side of the ammonia cooler 21 is connected with a cooling medium heat exchange unit; the cooling medium heat exchange unit comprises a flash evaporation device 24, a liquid phase outlet 27 of the flash evaporation device 24 is connected with a shell pass inlet of the ammonia cooler 21, a shell pass outlet of the ammonia cooler 21 is connected with a gas phase inlet 28 of the flash evaporation device 24, a gas phase inlet 29 of the flash evaporation device 24 is connected with a gas inlet 29 of a cooling medium compressor 25, and an outlet of the cooling medium compressor 25 is connected with a liquid phase inlet 30 of the flash evaporation device 24; the mechanical end of the cooling medium compressor 25 is connected to a steam turbine 26 with a steam line. The device is an elastic cold quantity adjusting device, namely the cooling medium heat exchange unit can adjust the cold quantity needed in the ammonia cooler 21 according to the amount of the introduced steam; the arrangement can be suitable for the purpose of normal operation of the synthetic ammonia system when the air separation device does not operate; that is, when the air separation plant is not operating, a large amount of steam needs to be supplied to satisfy the normal operation of the ammonia synthesis system, and when the air separation plant is operating, a small amount of steam needs to be supplied to satisfy the normal operation of the ammonia synthesis system.
The utility model discloses a theory of operation does: the utility model comprises two sets of production devices, namely an air separation device and a synthetic ammonia system; when the air separation plant does not operate, can guarantee ammonia synthesis device's normal operating, its operation process is: the raw material gas enters a circulating compressor 16 through a raw material gas pipeline 23 to be compressed, the compressed raw material gas enters an ammonia synthesis device 17 to carry out ammonia synthesis reaction, the gas after the reaction is cooled to about 40 ℃ after passing through byproduct steam and related matched heat exchange equipment (not shown), the heat is exchanged through a circulating water cooler 18 (and circulating water only passing through a water cooling tower 12), and the reaction gas is cooled to about 16 ℃; the gas temperature is reduced to about minus 2 ℃ after continuously passing through a reaction gas heat exchange device 19 and a separation device 20, and finally the gas temperature is reduced to about minus 10 ℃ again after passing through an ammonia cooler 21 and enters an ammonia storage tank 22; in the above process, the temperature of the circulating oil in the circulating compressor 16 (the cooling part of the circulating compressor 16 is cooled by the circulating water only through the water cooling tower 12) is about 40 ℃, and the circulating oil is continuously operated; when the cooling medium passes through the ammonia cooler 21, the cooling medium absorbs heat and becomes a gas state, the gas state is flashed through the flash evaporation device 24 and is sent to the cooling medium compressor 25, the gas state is compressed, the pressure is increased, the temperature is reduced and the liquid state is changed, and then the liquid state is sent to the flash evaporation device 24 for recycling; the medium pressure steam temperature consumed by the cooling medium compressor 25 in the normal production process is about 385 ℃ and 25 t/h.
When the air separation device operates, air is pressurized by a supercharger 1, precooled by a precooling device 2, decompressed by a decompressing device 3, rectified by a rectifying tower 4 and heat exchanged by a heat exchanging device 5, and then enters a storage tank 6; in the process, waste nitrogen generated by rectification in the rectifying tower 4 firstly enters the precooling device 2 to exchange heat with the pressurized air, enters the packed tower 7 after heat exchange and is in countercurrent contact with circulating water passing through the water cooling tower 12, and then is discharged out through the emptying noise reduction device 31; the temperature of circulating water passing through a water cooling tower 12 is 20-32 ℃, the temperature of the circulating water passing through a packing tower 7 is about 10 ℃, the pressure of the circulating water is increased by a second centrifugal pressure increasing pump 15 and is respectively conveyed to a cooling part of a circulating compressor 16 and a shell pass of a circulating water cooler 18 in an ammonia synthesis unit, the circulating water returns to the water cooling tower 12 to realize circulation, an ammonia synthesis system continuously operates while the circulating water operates, raw material gas enters the circulating compressor 16 through a raw material gas pipeline 23 to be compressed, the compressed raw material gas enters an ammonia synthesis device 17 to carry out ammonia synthesis reaction, and the reacted gas is cooled to about 20 ℃ after passing through by-product steam and related matched heat exchange equipment (not shown in the figure)The reaction gas is cooled to about 10 ℃ by heat exchange of a circulating water cooler 18; the gas temperature is reduced to about minus 5 ℃ after continuously passing through a reaction gas heat exchange device 19 and a separation device 20, and finally the gas temperature is reduced to about minus 10 ℃ again after passing through an ammonia cooler 21 and enters an ammonia storage tank 22; in the process, the temperature of the circulating oil in the circulating compressor 16 is about 35 ℃, and the circulating compressor continuously operates; when the cooling medium passes through the ammonia cooler 21, the cooling medium absorbs heat and becomes a gas state, the gas state is flashed through the flash evaporation device 24 and is sent to the cooling medium compressor 25, the gas state is compressed, the pressure is increased, the temperature is reduced and the liquid state is changed, and then the liquid state is sent to the flash evaporation device 24 for recycling; the temperature of the medium pressure steam consumed by the cooling medium compressor 25 in the normal production process is about 385 ℃ and 20 t/h; by comparison, the steam consumption of the steam turbine 26 is reduced by about 5t/h when the dirty nitrogen in the air conditioner is used; meanwhile, because the early-stage temperature is low and the cooling capacity is abundant, the separation device 20 can be completely separated, the net ammonia value of the system is high, the ammonia yield is improved, and the power consumption of the synthesis circulator is reduced by about 5 DEG/t NH3。
The above detailed description is only specific to the feasible embodiments of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent embodiments, modifications and improvements that do not depart from the technical scope of the present invention should be included in the scope of the present invention.
Claims (8)
1. The utility model provides a dirty nitrogen gas cold volume utilizes device in air separation plant, the device includes booster compressor (1), precooling apparatus (2), pressure relief device (3), rectifying column (4), heat transfer device (5) and storage tank (6) among the air separation plant, its characterized in that: a gas phase outlet at the top of the rectifying tower (4) is connected with a gas phase inlet (8) at the lower part of the packed tower (7) through a tube pass of the precooling device (2), a circulating water inlet (9) is arranged at the upper part of the packed tower (7), and a liquid phase outlet (10) at the bottom of the packed tower (7) is respectively connected with a cooling part of a circulating compressor (16) in the ammonia synthesis unit and a shell pass of a circulating water cooler (18).
2. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 1, characterized in that: and a gas phase outlet (11) at the top of the packed tower (7) is connected with a venting noise reduction device (31).
3. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 1, characterized in that: the cooling part of a circulating compressor (16) in the ammonia synthesis unit and the shell pass outlet of a circulating water cooler (18) are respectively connected with the inlet of a water cooling tower (12), and the outlet of the water cooling tower (12) is connected with the circulating water inlet (9) arranged at the upper part of a packed tower (7) through a first centrifugal booster pump (13);
the water cooling tower (12) is communicated with a dosing storage tank (14) with a valve.
4. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 1, characterized in that: and a liquid phase outlet (10) at the bottom of the packed tower (7) is respectively connected with a cooling part of a circulating compressor (16) in the ammonia synthesis unit and the shell side of a circulating water cooler (18) through a second centrifugal booster pump (15).
5. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 1, characterized in that: the ammonia synthesis unit comprises a circulating compressor (16), an inlet of the circulating compressor (16) is connected with a raw material gas pipeline (23), and a gas-phase outlet of the circulating compressor (16) is connected with an ammonia storage tank (22) through tube passes of an ammonia synthesis device (17), a circulating water cooler (18), a reaction gas heat exchange device (19), a separation device (20) and an ammonia cooler (21) in sequence.
6. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 5, characterized in that: and a gas phase outlet at the top of the reaction gas heat exchange device (19) is connected with a raw material gas pipeline (23).
7. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 5, characterized in that: the liquid phase outlet of the separation device (20) is connected with the inlet of an ammonia storage tank (22).
8. The apparatus for utilizing the cooling capacity of the waste nitrogen gas in the air separation plant according to claim 5, characterized in that: the shell side of the ammonia cooler (21) is connected with a cooling medium heat exchange unit;
the cooling medium heat exchange unit comprises a flash evaporation device (24), a liquid phase outlet (27) of the flash evaporation device (24) is connected with a shell side inlet of the ammonia cooler (21), a shell side outlet of the ammonia cooler (21) is connected with a gas phase inlet (28) of the flash evaporation device (24), a gas phase inlet (29) of the flash evaporation device (24) is connected with a gas inlet (29) of a cooling medium compressor (25), and an outlet of the cooling medium compressor (25) is connected with a liquid phase inlet (30) of the flash evaporation device (24);
the mechanical end of the cooling medium compressor (25) is connected with a steam turbine (26) with a steam pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120942688.0U CN215113526U (en) | 2021-04-30 | 2021-04-30 | Dirty nitrogen cooling capacity utilization device in air separation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120942688.0U CN215113526U (en) | 2021-04-30 | 2021-04-30 | Dirty nitrogen cooling capacity utilization device in air separation device |
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| CN215113526U true CN215113526U (en) | 2021-12-10 |
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| CN202120942688.0U Active CN215113526U (en) | 2021-04-30 | 2021-04-30 | Dirty nitrogen cooling capacity utilization device in air separation device |
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2021
- 2021-04-30 CN CN202120942688.0U patent/CN215113526U/en active Active
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