CN219283781U - Nitrogen making equipment for preparing high-purity oxygen - Google Patents
Nitrogen making equipment for preparing high-purity oxygen Download PDFInfo
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- CN219283781U CN219283781U CN202223224534.1U CN202223224534U CN219283781U CN 219283781 U CN219283781 U CN 219283781U CN 202223224534 U CN202223224534 U CN 202223224534U CN 219283781 U CN219283781 U CN 219283781U
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- oxygen
- tower
- nitrogen
- rectifying tower
- purity
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 93
- 239000001301 oxygen Substances 0.000 title claims abstract description 93
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 93
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 50
- 238000000605 extraction Methods 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000002912 waste gas Substances 0.000 claims description 18
- 238000010992 reflux Methods 0.000 claims description 8
- 238000000746 purification Methods 0.000 claims description 5
- 238000004088 simulation Methods 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 9
- 239000002994 raw material Substances 0.000 description 7
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 238000001816 cooling Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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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
- F25J3/04406—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
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
-
- 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/0423—Subcooling of liquid process streams
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
Landscapes
- 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 high-purity oxygen and nitrogen production equipment, and in particular discloses nitrogen production equipment for preparing high-purity oxygen, which comprises a main heat exchanger, a rectifying tower, a condenser, a high-purity oxygen tower, a subcooler, an evaporator and an expander, wherein the main heat exchanger is arranged in a cold box, an air outlet of the main heat exchanger is communicated with an air inlet at the lower part of the rectifying tower through a pipeline, a liquid air outlet at the bottom of the rectifying tower is sequentially communicated with a liquid air inlet of the subcooler and a liquid air inlet of the condenser through a pipeline, an oxygen-enriched liquid air extraction port is arranged in the middle part of the rectifying tower, and a liquid oxygen outlet at the bottom of the high-purity oxygen tower is connected with a user end through a pipeline. The utility model can extract high-purity oxygen in the single-tower nitrogen production equipment for producing high-purity nitrogen, the configuration equipment is greatly reduced, the number of connected low-temperature pipelines and valves is also greatly reduced, the operation reliability of the equipment is high, the process route is short, the occupied area of the cold box is reduced, and the manufacturing cost is reduced.
Description
Technical Field
The utility model relates to the field of high-purity oxygen and nitrogen production equipment, in particular to nitrogen production equipment for preparing high-purity oxygen.
Background
In the prior art, a plurality of methods such as water electrolysis, low-temperature rectification, adsorption, membrane separation and the like are adopted to prepare oxygen with higher purity, most commercial oxygen is manufactured and produced in air separation equipment, high-purity oxygen is obtained after air is liquefied and purified by low-temperature rectification, a small amount of oxygen is also adopted as raw material, high-purity oxygen with purity of more than 99.99% can be prepared by catalytic dehydrogenation, the equipment of the technical scheme is comparatively more, the related process route is longer, the manufacturing cost is comparatively high, and in addition, a heavy component removing tower is required to be added outside a conventional nitrogen-making rectification tower to extract the high-purity oxygen, so that the investment of equipment is also increased, and the method is quite uneconomical.
Therefore, based on the related concept that the equipment investment can be reduced and the nitrogen and the high-purity oxygen can be simultaneously extracted, the design of the single-tower nitrogen making equipment can extract the high-purity oxygen.
Disclosure of Invention
The utility model aims to provide the nitrogen production equipment for preparing high-purity oxygen, and by the design of the utility model, the high-purity oxygen can be extracted in the single-tower nitrogen production equipment for producing high-purity nitrogen, only one rectifying tower and one high-purity oxygen tower are needed, the configuration equipment is greatly reduced, the number of connected low-temperature pipelines and valves is greatly reduced, the operation reliability of the equipment is high, the process route is short, the occupied area of a cold box is reduced, and the manufacturing cost is reduced.
In order to solve the technical problems, the utility model provides nitrogen production equipment for producing high-purity oxygen, which comprises a main heat exchanger, a rectifying tower, a condenser, a high-purity oxygen tower, a subcooler, an evaporator and an expander, wherein the main heat exchanger, the rectifying tower, the condenser, the high-purity oxygen tower, the subcooler, the evaporator and the expander are arranged in a cold box;
the air inlet of the main heat exchanger is an air delivery port after filtration and purification, the air outlet of the main heat exchanger is communicated with the air inlet at the lower part of the rectifying tower through a pipeline, the bottom liquid air outlet of the rectifying tower is communicated with the liquid air inlet of the subcooler, the liquid air inlet of the rectifying tower and the liquid air inlet of the condenser in sequence through pipelines,
the oxygen-enriched waste gas outlet of the condenser is sequentially communicated with the subcooler and the oxygen-enriched waste gas inlet of the main heat exchanger through a pipeline, the oxygen-enriched waste gas outlet of the main heat exchanger is communicated with the oxygen-enriched waste gas inlet of the expander, the oxygen-enriched waste gas outlet of the expander is communicated with the oxygen-enriched waste gas inlet of the main heat exchanger through a pipeline,
the middle part of the rectifying tower is provided with an oxygen-enriched liquid air extraction port, the extraction port is sequentially communicated with an oxygen-enriched liquid air inlet of the subcooler and an oxygen-enriched liquid air inlet at the upper part of the high-purity oxygen tower through a pipeline, an oxygen outlet at the top of the high-purity oxygen tower is communicated with an oxygen inlet of the main heat exchanger through a pipeline, and a liquid oxygen outlet at the bottom of the high-purity oxygen tower is connected with a user end through a pipeline;
and a high-purity nitrogen outlet at the upper part of the rectifying tower is respectively communicated with the high-purity nitrogen inlet of the main heat exchanger and the evaporator through pipelines.
Further, a liquid nitrogen outlet at the bottom of the condenser is connected with a reflux liquid inlet at the upper part of the rectifying tower through a pipeline.
Furthermore, the oxygen-enriched liquid air extraction port of the rectifying tower calculates the extraction position through simulation.
Further, a liquid nitrogen outlet of the evaporator is communicated with a reflux liquid inlet at the upper part of the rectifying tower through a pipeline.
Furthermore, the high-purity oxygen tower is a novel regular metal packed tower or a sieve plate tower.
The beneficial effects of the utility model are as follows:
1. through the design of the utility model, high-purity oxygen can be extracted in single-tower nitrogen production equipment for producing high-purity nitrogen, only one rectifying tower and one high-purity oxygen tower are needed, configuration equipment is greatly reduced, connected low-temperature pipelines and valves are also greatly reduced, the operation reliability of the equipment is high, the process route is short, the occupied area of a cold box is reduced, and the manufacturing cost is reduced.
2. According to the utility model, the oxygen-enriched liquid air extraction port is designed in the middle of the rectifying tower, so that high-purity oxygen raw material gas can be extracted in the process of preparing nitrogen by single-tower rectification, the rectification working condition of the rectifying tower can be obviously improved, and the extraction rate and purity of nitrogen are improved; the position of the oxygen-enriched liquid-air extraction port is calculated by simulation, so that the liquid-air weight components (AR, CH 4) of the extraction port are the least and the oxygen content is the highest, and the purity of the high-purity oxygen is higher.
Drawings
In order to more clearly illustrate the technical solutions of the present utility model, the following description will briefly explain the drawings used in the embodiments or the description of the prior art, and it is obvious that the drawings in the following description are only some embodiments of the present utility model, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a nitrogen plant for producing high purity oxygen according to the present utility model;
in the figure: 1-cold box, 2-main heat exchanger, 3-rectifying tower, 4-condenser, 5-high purity oxygen tower, 6-subcooler, 7-evaporator and 8-expander.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all embodiments of the utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In one embodiment of the present utility model, as shown in fig. 1, a nitrogen production apparatus for producing high purity oxygen comprises a main heat exchanger 2, a rectifying tower 3, a condenser 4, a high purity oxygen tower 5, a subcooler 6, an evaporator 7 and an expander 8 which are arranged in a cold box 1, wherein the condenser 4 is arranged above the rectifying tower 3, and the evaporator 7 is arranged below the high purity oxygen tower 5; the high purity oxygen column 5 is a novel regular metal packed column or a sieve plate column.
The air inlet of the main heat exchanger 2 is an air delivery port after filtration and purification, the air outlet is communicated with the air inlet at the lower part of the rectifying tower 3 through a pipeline,
the bottom liquid air outlet of the rectifying tower 3 is sequentially communicated with the liquid air inlet of the subcooler 6, the liquid air inlet of the rectifying tower 3 and the liquid air inlet of the condenser 4 through pipelines, the oxygen-enriched waste gas outlet of the condenser 4 is sequentially communicated with the subcooler 6 and the oxygen-enriched waste gas inlet of the main heat exchanger 2 through pipelines, the oxygen-enriched waste gas outlet of the main heat exchanger 2 is communicated with the oxygen-enriched waste gas inlet of the expander 8, the oxygen-enriched waste gas outlet of the expander 8 is communicated with the oxygen-enriched waste gas inlet of the main heat exchanger 2 through pipelines,
the middle part of the rectifying tower 3 is provided with an oxygen-enriched liquid air extraction port, the oxygen-enriched liquid air extraction port calculates an extraction position through simulation, the extraction port is sequentially communicated with an oxygen-enriched liquid air inlet of the subcooler 6 and an oxygen-enriched liquid air inlet at the upper part of the high-purity oxygen tower 5 through a pipeline, an oxygen outlet at the top of the high-purity oxygen tower 5 is communicated with an oxygen inlet of the main heat exchanger 2 through a pipeline, and a liquid oxygen outlet at the bottom of the high-purity oxygen tower 5 is connected with a user end through a pipeline;
the high-purity nitrogen outlet at the upper part of the rectifying tower 3 is respectively communicated with the high-purity nitrogen inlets of the main heat exchanger 2 and the evaporator 7 through pipelines, the liquid nitrogen outlet of the evaporator 7 is communicated with the reflux liquid inlet at the upper part of the rectifying tower 3 through a pipeline, and the liquid nitrogen outlet at the bottom of the condenser 4 is communicated with the reflux liquid inlet at the upper part of the rectifying tower 3 through a pipeline.
The working flow of the utility model is as follows:
inputting a compressed air raw material which is dried and clean after being subjected to molecular sieve adsorption pre-purification into an air inlet of a main heat exchanger 2, cooling and cooling the compressed air raw material by the main heat exchanger 2, enabling the compressed air raw material to enter the rectifying tower 3 from the air inlet at the lower part of the rectifying tower 3 to participate in rectification, obtaining high-purity nitrogen at the top of the rectifying tower 3, and sending the high-purity nitrogen to a user side after heat exchange and temperature rise recovery of the main heat exchanger 2; in addition, the heat source of the high purity oxygen column 5 adopts nitrogen gas of the rectifying column 3, specifically, a high purity nitrogen gas inlet of the evaporator 7 is connected with a high purity nitrogen gas outlet at the upper part of the rectifying column 3, and the nitrogen gas is condensed and returned to a liquid nitrogen reflux liquid inlet of the rectifying column 3 as reflux liquid of the rectifying column 3.
In addition, liquid air is extracted from a liquid air outlet at the bottom of the rectifying tower 3, and is sent into a condenser 4 to be used as a cold source after being supercooled by a supercooler 6, and is evaporated and then enters the supercooler 6 to enter a main heat exchanger 2, and the liquid air is divided into two paths in the main heat exchanger 2, wherein one path is discharged out of a cold box after heat exchange, heating and cold recovery are continued; the other path of the cold energy is expanded by an expander 8, most of the cold energy required by the generating equipment enters the main heat exchanger 2, the heat exchange and the temperature rise are continued, and the cold energy is recovered and then is discharged out of the cold box 1 to be used as regeneration gas of the front-end pre-purification treatment system.
The high-purity oxygen process raw material liquid is extracted from an oxygen-enriched liquid air extraction port in the middle of the rectifying tower 3, the rectifying working condition of the rectifying tower 3 is improved, the extraction rate and purity of nitrogen are improved, the extracted high-purity oxygen process raw material liquid enters the top of the high-purity oxygen tower 5, and qualified high-purity oxygen products are obtained at the bottom of the high-purity oxygen tower 5 through gradual rectification, and are sent to a user side after being discharged from a cold box.
The above disclosure is only a preferred embodiment of the present utility model, and it is needless to say that the scope of the utility model is not limited thereto, and therefore, the equivalent changes according to the claims of the present utility model still fall within the scope of the present utility model.
Claims (5)
1. The nitrogen production equipment for preparing high-purity oxygen is characterized by comprising a main heat exchanger (2), a rectifying tower (3), a condenser (4), a high-purity oxygen tower (5), a subcooler (6), an evaporator (7) and an expander (8) which are arranged in a cold box (1), wherein the condenser (4) is arranged above the rectifying tower (3), and the evaporator (7) is arranged below the Gao Chunyang tower (5);
the air inlet of the main heat exchanger (2) is an air delivery port after filtration and purification, the air outlet is communicated with the air inlet at the lower part of the rectifying tower (3) through a pipeline,
the bottom liquid air outlet of the rectifying tower (3) is communicated with the liquid air inlet of the subcooler (6), the liquid air inlet of the rectifying tower (3) and the liquid air inlet of the condenser (4) in sequence through pipelines,
the oxygen-enriched waste gas outlet of the condenser (4) is sequentially communicated with the subcooler (6) and the oxygen-enriched waste gas inlet of the main heat exchanger (2) through a pipeline, the oxygen-enriched waste gas outlet of the main heat exchanger (2) is communicated with the oxygen-enriched waste gas inlet of the expander (8), the oxygen-enriched waste gas outlet of the expander (8) is communicated with the oxygen-enriched waste gas inlet of the main heat exchanger (2) through a pipeline,
the middle part of the rectifying tower (3) is provided with an oxygen-enriched liquid air extraction port, the extraction port is sequentially communicated with an oxygen-enriched liquid air inlet of the subcooler (6) and an oxygen-enriched liquid air inlet at the upper part of the Gao Chunyang tower (5) through a pipeline, an oxygen outlet at the top of the Gao Chunyang tower (5) is communicated with an oxygen inlet of the main heat exchanger (2) through a pipeline, and a liquid oxygen outlet at the bottom of the Gao Chunyang tower (5) is connected with a user end through a pipeline;
the high-purity nitrogen outlet at the upper part of the rectifying tower (3) is respectively communicated with the high-purity nitrogen inlet of the main heat exchanger (2) and the evaporator (7) through pipelines.
2. The nitrogen production equipment for producing high-purity oxygen according to claim 1, wherein the liquid nitrogen outlet at the bottom of the condenser (4) is connected with the reflux liquid inlet at the upper part of the rectifying tower (3) through a pipeline.
3. The nitrogen production equipment for producing high-purity oxygen according to claim 1, wherein the oxygen-enriched liquid air extraction port of the rectifying tower (3) calculates the extraction position through simulation.
4. Nitrogen plant for the production of high purity oxygen according to claim 1 or 2, characterized in that the liquid nitrogen outlet of the evaporator (7) is connected to the reflux liquid inlet in the upper part of the rectifying column (3) by means of a pipe.
5. The nitrogen making apparatus for making high purity oxygen according to claim 1, wherein said Gao Chunyang column (5) is a novel structured metal packed column or a sieve tray column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223224534.1U CN219283781U (en) | 2022-12-02 | 2022-12-02 | Nitrogen making equipment for preparing high-purity oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223224534.1U CN219283781U (en) | 2022-12-02 | 2022-12-02 | Nitrogen making equipment for preparing high-purity oxygen |
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| Publication Number | Publication Date |
|---|---|
| CN219283781U true CN219283781U (en) | 2023-06-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223224534.1U Active CN219283781U (en) | 2022-12-02 | 2022-12-02 | Nitrogen making equipment for preparing high-purity oxygen |
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| Country | Link |
|---|---|
| CN (1) | CN219283781U (en) |
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- 2022-12-02 CN CN202223224534.1U patent/CN219283781U/en active Active
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