CN102445054A - Process for preparing oxygen and nitrogen by air separation - Google Patents
Process for preparing oxygen and nitrogen by air separation Download PDFInfo
- Publication number
- CN102445054A CN102445054A CN2011104349408A CN201110434940A CN102445054A CN 102445054 A CN102445054 A CN 102445054A CN 2011104349408 A CN2011104349408 A CN 2011104349408A CN 201110434940 A CN201110434940 A CN 201110434940A CN 102445054 A CN102445054 A CN 102445054A
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- Prior art keywords
- oxygen
- nitrogen
- air
- rectifying
- rectifying column
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Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 169
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 93
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 239000001301 oxygen Substances 0.000 title claims abstract description 91
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 82
- 238000000926 separation method Methods 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title abstract description 3
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 25
- 238000005516 engineering process Methods 0.000 claims description 20
- 239000007789 gas Substances 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 9
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 8
- 230000008929 regeneration Effects 0.000 claims description 8
- 238000011069 regeneration method Methods 0.000 claims description 8
- 230000000630 rising effect Effects 0.000 claims description 7
- 239000002912 waste gas Substances 0.000 claims description 7
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 5
- 238000004821 distillation Methods 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000000605 extraction Methods 0.000 abstract description 3
- 238000002360 preparation method Methods 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 7
- 238000000034 method Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229920000049 Carbon (fiber) Polymers 0.000 description 1
- 239000004917 carbon fiber Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 1
- 229920005591 polysilicon Polymers 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
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
- F25J3/04248—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
- 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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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 invention belongs to the technical field of air separation, and particularly relates to a process for preparing oxygen and nitrogen by air separation. And cooling the purified air to saturation temperature, then, rectifying the air in a three-stage rectification system, obtaining a product nitrogen at the top of an upper rectification tower and a product oxygen at the lower part of an oxygen tower after rectification. The nitrogen preparation process has low discharge pressure (0.5-1.0 Mpa) of the air compressor and low energy consumption, greatly reduces the energy consumption requirement of the air separation nitrogen preparation device, meets the current national requirements on energy conservation and emission reduction of high energy consumption industries, and simultaneously has the nitrogen extraction rate of 55-75 percent and the oxygen extraction rate of 60-75 percent.
Description
Technical field
The invention belongs to the air separation technology field, particularly a kind of technology of producing oxygen and nitrogen by air separation.
Background technology
Along with The development in society and economy, in recent years, the application of high-purity nitrogen plant is constantly expanded, and all has like industries such as petrochemical industry, glass, rubber, building board, polysilicon, carbon fibers to set foot in.Industry is ever-increasing to the demand of nitrogen and oxygen, simultaneously to the energy-saving and cost-reducing also constantly higher requirement of proposition.Therefore, want on market, to occupy whip hand, just must improve product extraction rate, reduce the operation energy consumption of device, the energy-saving potential of excavating equipment operation makes full use of air simultaneously as far as possible, extracts wherein nitrogen and air simultaneously.
Summary of the invention
The object of the present invention is to provide and a kind ofly produce the technology of oxygen and nitrogen, overcome that present handicraft product recovery rate is low, the bigger defective of device operation energy consumption by air separation.
The technical scheme that the present invention adopts is following:
A kind of technology of producing oxygen and nitrogen by air separation; Three grades of distillation systems of entering carried out rectifying after cleaned air passes was cooled to saturation temperature; Described three grades of distillation systems by the two-stage rectification system and the oxygen column after being connected in the two-stage rectification system constitute, described two-stage rectification system is made up of with following rectifying column the last rectifying column that condenser/evaporator connects as one, after the rectifying; Obtain product nitrogen gas at last rectifying column top, obtain product oxygen in the oxygen column bottom.
The following rectifying column of entering carried out rectifying after cleaned air passes was cooled to saturation temperature, obtained nitrogen at following rectifying column top, obtained oxygen-enriched liquid air in the bottom.
Can air be carried out removal of impurities, compression, precooling operation successively before purifying.
The preparation process of product nitrogen gas is specially: the nitrogen that following rectifying column top obtains is divided into A, B two parts; The condenser/evaporator that A partly gets into the rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1 and A2 two parts simultaneously; Wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation, and the nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature.
A2 partly gets into down the top of rectifying column as phegma.
The evaporimeter that B part nitrogen gets into the oxygen column bottom as thermal source and in evaporimeter by the liquid oxygen of oxygen column bottom be cooled to liquid nitrogen get under the top of rectifying column as phegma.
Wherein, in the nitrogen that following rectifying column top obtains, the nitrogen amount of B part is decided based on oxygen column bottom rising quantity of steam, and all the other then are the A part; Among the A, the nitrogen amount of A2 part is based on rectifying column nitrogen output and purity decision down, and all the other then are A1.
The oxygen that produces in the oxygen column bottom is delivered to the user as product gas behind main heat exchanger re-heat to normal temperature.
Further; Cross cold deutomerite at the oxygen-enriched liquid air of rectifier bottoms generation down through subcooler and flow into the rectifying column middle part; The oxygen-enriched liquid air throttling that produces in last rectifier bottoms gets into the oxygen column top as the oxygen column phegma, and the oxygen column bottom evaporimeter phase-change heat-exchange of liquid oxygen through the oxygen column bottom produces oxygen as rising steam.
Raw air is compressed to 0.5～1.0MPa (G) by air compressor after air cleaner is removed dust in air and impurity, reducing air themperature through chilldown system again is 5-8 ℃.
The dirty nitrogen that last rectifier produces goes out tower after get into the turbo-expander expansion after subcooler and the main heat exchanger re-heat; Direct regeneration gas after also getting into the turbo-expander expansion or get into the heat exchanger re-heat after the waste gas entering heat exchanger re-heat at oxygen column top as purification system.
Expansion is mended and is increased cold to turbo-expander, and the dirty nitrogen after the expansion reclaims the regeneration gas of cold rear section as purification system through main heat exchanger, and all the other diffuse.
Below set forth the technology that the present invention produces nitrogen and oxygen simultaneously from another angle again:
Raw air is removed dust in air and impurity through air cleaner, is compressed to 0.5～1.0MPa (G) by air compressor then, and reducing air themperature through chilldown system again is 5-8 ℃, gets into purification system after separating free water, removes H
2O, CO
2, C
2H
2And other hydrocarbon.Cleaned air passes is carried out heat exchange and is got into down the rectifying column bottom after being cooled to saturation temperature and carry out rectifying through main heat exchanger and the waste gas that backflows and nitrogen, oxygen, obtains nitrogen at rectifying column top down.
Nitrogen separated into two parts after the rectifying: a part (said A part promptly) gets into condenser/evaporator as thermal source; The oxygen-enriched liquid air of rectifier bottoms is cooled to liquid nitrogen on the quilt in condenser/evaporator; Be divided into two parts: wherein the top of rectifying column is as phegma under a part of (being the A2 part) entering, and a part (being the A1 part) liquid nitrogen is crossed cold deutomerite through subcooler and flowed into the rectifying column top as upward tower rectifying of phegma participation (partly can be used as nitrogen products takes out) in addition; A part of in addition nitrogen (being the B part) gets into the evaporimeter of oxygen column bottom as thermal source, and the top of in evaporimeter, being cooled off rectifying column under the entering by the liquid oxygen of oxygen column bottom is as phegma.
Rectifying column middle part on the oxygen-enriched liquid air that following rectifier bottoms obtains is crossed through subcooler that cold back throttling is laggard and gone into; The oxygen-enriched liquid air of condenser/evaporator bottom is heated as the rising steam of oxygen-enriched air as last rectifying column by the nitrogen by rectifying column top generation down; Last rectifying column is through after the rectifying; Obtain sending the user after product nitrogen gas process subcooler and the main heat exchanger re-heat at its top, take out dirty nitrogen at last rectifier and after subcooler and main heat exchanger re-heat, get into decompressor.
The oxygen-enriched liquid air of last rectifier bottoms takes out through getting into the oxygen column top after the throttling as phegma; Liquid oxygen in the evaporimeter of oxygen column bottom is that oxygen is as rising steam by the vaporized nitrogen by following rectifying column; The bottom produces oxygen and after the main heat exchanger re-heat, send the user after the process rectifying; The waste gas at top is joined and is expanded by entering decompressor after the dirty nitrogen entering heat exchanger re-heat of last rectifying column generation; Increase cold to the device benefit, the dirty nitrogen after the expansion reclaims the regeneration gas of cold rear section as purification system through main heat exchanger, and all the other diffuse.
Wherein also can do following adjustment based on arts demand:
1. go into main heat exchanger cooling back and get into rectifying column down through the booster expansion turbine supercharging is laggard through the part air that purifies.
2. the waste gas that produces of adjustment oxygen column directly gets into after the main heat exchanger re-heat as regeneration gas.
The recovery rate of the above-mentioned technology nitrogen of the present invention is 55-75%, and the nitrogen pressure of acquisition (being nitrogen product requirement pressure) is 0.2～0.35MPa (G), in the nitrogen 0
2≤1-100ppm.The recovery rate of oxygen is 60-75%, and the oxygen pressure of acquisition (being oxygen product requirement pressure) is 0.005～0.25MPa (G), oxygen content 80%-99.6%.Process energy consumption is 0.17-0.25 kWh/Nm
3(N
2+ O
2).
In the technology, concrete reflux ratio and other each parameters can be adjusted according to the situation of concrete rectifying column and oxygen column by those skilled in the art, also can assist means such as existing simulation softward, set forth no longer one by one here.
The present invention has following advantage with respect to prior art:
Nitrogen reparation technology air compressor of the present invention row pressure low (0.5-1.0Mpa); Energy consumption is low; Greatly reduce the energy consumption requirement of nitrogen production by air separation device; Meet the requirement of the present energy-saving and emission-reduction to high energy-consuming industry of country, the nitrogen recovery rate can reach 55-75% simultaneously, and the recovery rate of oxygen is 60-75%.
Description of drawings
Fig. 1 is produced the process chart of oxygen and nitrogen by air separation for embodiment 1.
The specific embodiment
Below with specific embodiment technical scheme of the present invention is described, but protection scope of the present invention is not limited thereto:
Embodiment 1
It is 0.3MPa (gauge pressure is all represented with gauge pressure with downforce) that this routine nitrogen product requires pressure, and it is 0.15MPa that oxygen product requires pressure.
In conjunction with Fig. 1, raw air is removed dust in air and impurity through air cleaner 1, be compressed to 0.8MPa by air compressor 2 then after, reduce air themperatures to 5-8 ℃ through chilldown system 3 again, get into purification system after separating free water, remove H
2O, CO
2, C
2H
2And other hydrocarbon.Cleaned air passes is carried out heat exchange and is cooled to saturation temperature through main heat exchanger 5 and the waste gas that backflows and nitrogen, oxygen, and the back gets into down rectifying column 6 bottoms and carries out rectifying, obtains nitrogen at rectifying 6 tops of tower down.
Nitrogen separated into two parts after the rectifying: wherein 55% nitrogen gets into condenser/evaporator 7 as thermal source; The oxygen-enriched liquid air of rectifying column 8 bottoms is cooled to liquid nitrogen on the quilt in condenser/evaporator 7; Be divided into two parts: wherein the top of rectifying column 6 is as phegma under 30% entering, and other 70% liquid nitrogen is crossed cold deutomerite through subcooler 9 and flowed into rectifying column 8 tops as upward tower rectifying of phegma participation (partly can be used as nitrogen products takes out); The evaporimeter that rectifying column 6 tops obtain nitrogen (45%) entering oxygen column 10 bottoms under all the other is as thermal source, and the top of in evaporimeter, being cooled off rectifying column 6 under the entering by the liquid oxygen of oxygen column 10 bottoms is as phegma.
Rectifying column 8 middle parts on the oxygen-enriched liquid air that obtains in following rectifying column 6 bottoms is crossed through subcooler 9 that cold back throttling is laggard and gone into; The oxygen-enriched liquid air of condenser/evaporator bottom is heated as the rising steam of oxygen-enriched air as last rectifying column 8 by the nitrogen by rectifying column 6 tops generation down; Through after the rectifying; Obtain sending the user after product nitrogen gas (0.3MPa) process subcooler 9 and main heat exchanger 5 re-heats at last rectifying column 8 tops, take out dirty nitrogen on last rectifying column 8 tops and after subcooler 9 and main heat exchanger 5 re-heats, get into decompressor 11.
The oxygen-enriched liquid air (containing oxygen 65.6%) of last rectifying column 8 bottoms takes out through getting into oxygen column 10 tops after the throttling as phegma; Liquid oxygen in the oxygen column 10 bottom evaporimeters is that oxygen is as rising steam by the vaporized nitrogen by following rectifying column 6; Through the rectifying rear lower produce oxygen (0.15MPa) after main heat exchanger 5 re-heats, send the user, the waste gas at top is directly as the purification system regeneration gas; Get into decompressor 11 after dirty nitrogen entering heat exchanger 5 re-heats by last rectifying column 8 generations and expand, increase cold to the device benefit, the dirty nitrogen after the expansion is the regeneration gas as purification system through main heat exchanger 5 recovery cold rear sections, and all the other diffuse.
The nitrogen recovery rate is 63%, and the recovery rate of oxygen is 71%, and energy consumption is 0.193 kWh/Nm
3(N
2+ O
2).
The foregoing description is the preferred embodiment of the present invention, but embodiment of the present invention is not restricted to the described embodiments, and other the change that any the present invention of not deviating from did all should be the substitute mode of equivalence, is included within protection scope of the present invention.
Claims (10)
1. technology of producing oxygen and nitrogen by air separation; It is characterized in that cleaned air passes is cooled to and gets into three grades of distillation systems after the saturation temperature and carry out rectifying, described three grades of distillation systems by the two-stage rectification system and the oxygen column after being connected in the two-stage rectification system constitute; Described two-stage rectification system is made up of with following rectifying column the last rectifying column that condenser/evaporator connects as one; After the rectifying, obtain product nitrogen gas, obtain product oxygen in the oxygen column bottom at last rectifying column top.
2. as claimed in claim 1ly produce the technology of oxygen and nitrogen by air separation, it is characterized in that, cleaned air passes is cooled to and gets into down after the saturation temperature that rectifying column carries out rectifying, obtains nitrogen at rectifying column top down, obtains oxygen-enriched liquid air in the bottom.
3. the technology of producing oxygen and nitrogen by air separation as claimed in claim 2; It is characterized in that; The nitrogen that following rectifying column top obtains is divided into A, B two parts; The condenser/evaporator that A partly gets into the rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1 and A2 two parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation, and the nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature.
4. as claimed in claim 3ly produce the technology of oxygen and nitrogen, it is characterized in that A2 partly gets into down the top of rectifying column as phegma by air separation.
5. the technology of producing oxygen and nitrogen by air separation as claimed in claim 3; It is characterized in that the top of rectifying column was as phegma under the evaporimeter that B part nitrogen gets into the oxygen column bottom was got into by the liquid oxygen cooling of oxygen column bottom as thermal source and in evaporimeter.
6. as claimed in claim 3ly produce the technology of oxygen and nitrogen, it is characterized in that the oxygen that produces in the oxygen column bottom is delivered to the user as product gas behind main heat exchanger re-heat to normal temperature by air separation.
7. the technology of producing oxygen and nitrogen by air separation as claimed in claim 6; It is characterized in that; Cross cold deutomerite at the oxygen-enriched liquid air of rectifier bottoms generation down through subcooler and flow into the rectifying column middle part; The oxygen-enriched liquid air throttling that produces in last rectifier bottoms gets into the oxygen column top as the oxygen column phegma, and the oxygen column bottom evaporimeter phase-change heat-exchange of liquid oxygen through the oxygen column bottom produces oxygen as rising steam.
8. like the described technology of producing oxygen and nitrogen by air separation of one of claim 3-7; Raw air is compressed to 0.5～1.0MPa (G) by air compressor after air cleaner is removed dust in air and impurity; Reducing air themperature through chilldown system again is 5-8 ℃, purifies then.
9. as claimed in claim 8ly produce the technology of oxygen and nitrogen, it is characterized in that the dirty nitrogen that last rectifier produces goes out tower after get into the turbo-expander expansion after subcooler and the main heat exchanger re-heat by air separation; Direct regeneration gas after also getting into the turbo-expander expansion or get into the heat exchanger re-heat after the waste gas entering heat exchanger re-heat at oxygen column top as purification system.
10. as claimed in claim 9ly produce the technology of oxygen and nitrogen by air separation, it is characterized in that, mend to turbo-expander and increase cold, the dirty nitrogen after the expansion reclaims the regeneration gas of cold rear section as purification system through main heat exchanger, and all the other diffuse.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104349408A CN102445054A (en) | 2011-12-22 | 2011-12-22 | Process for preparing oxygen and nitrogen by air separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104349408A CN102445054A (en) | 2011-12-22 | 2011-12-22 | Process for preparing oxygen and nitrogen by air separation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102445054A true CN102445054A (en) | 2012-05-09 |
Family
ID=46007790
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011104349408A Pending CN102445054A (en) | 2011-12-22 | 2011-12-22 | Process for preparing oxygen and nitrogen by air separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102445054A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102706101A (en) * | 2012-05-23 | 2012-10-03 | 苏州制氧机有限责任公司 | Air separating device |
| CN103438663A (en) * | 2013-07-11 | 2013-12-11 | 开封黄河空分集团有限公司 | Device and process for preparing high-purity oxygen and nitrogen under ultra-low pressure |
| CN106185843A (en) * | 2016-06-29 | 2016-12-07 | 芜湖杨燕制药有限公司 | Medical nitrogen making machine |
| CN112062095A (en) * | 2020-09-21 | 2020-12-11 | 江苏双泰阀机械有限公司 | Double-air-passage mixed flow oxygen and nitrogen making machine |
| CN113883829A (en) * | 2021-11-01 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Method for preparing high-purity nitrogen with low energy consumption and method for preparing high-purity nitrogen with low energy consumption |
| WO2022238385A1 (en) * | 2021-05-11 | 2022-11-17 | Tecforlime | Decarbonation process of carbonated materials in a multi-shaft vertical kiln |
| WO2022238387A1 (en) * | 2021-05-11 | 2022-11-17 | Tecforlime | Decarbonation process of carbonated materials in a multi-shaft vertical kiln |
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-
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|---|---|---|---|---|
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| CN103438663A (en) * | 2013-07-11 | 2013-12-11 | 开封黄河空分集团有限公司 | Device and process for preparing high-purity oxygen and nitrogen under ultra-low pressure |
| CN106185843A (en) * | 2016-06-29 | 2016-12-07 | 芜湖杨燕制药有限公司 | Medical nitrogen making machine |
| CN106185843B (en) * | 2016-06-29 | 2018-08-07 | 芜湖杨燕制药有限公司 | Medical nitrogen making machine |
| CN112062095A (en) * | 2020-09-21 | 2020-12-11 | 江苏双泰阀机械有限公司 | Double-air-passage mixed flow oxygen and nitrogen making machine |
| WO2022238385A1 (en) * | 2021-05-11 | 2022-11-17 | Tecforlime | Decarbonation process of carbonated materials in a multi-shaft vertical kiln |
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| CN113883829A (en) * | 2021-11-01 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Method for preparing high-purity nitrogen with low energy consumption and method for preparing high-purity nitrogen with low energy consumption |
| CN113883829B (en) * | 2021-11-01 | 2023-02-28 | 四川空分设备(集团)有限责任公司 | Method and device for preparing high-purity nitrogen with low energy consumption |
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Application publication date: 20120509 |