CN102721261A - Method for producing low purity oxygen with pressure and high purity nitrogen with pressure by adopting reflux expansion refrigeration - Google Patents
Method for producing low purity oxygen with pressure and high purity nitrogen with pressure by adopting reflux expansion refrigeration Download PDFInfo
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- CN102721261A CN102721261A CN2012101253037A CN201210125303A CN102721261A CN 102721261 A CN102721261 A CN 102721261A CN 2012101253037 A CN2012101253037 A CN 2012101253037A CN 201210125303 A CN201210125303 A CN 201210125303A CN 102721261 A CN102721261 A CN 102721261A
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 205
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 101
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 48
- 239000001301 oxygen Substances 0.000 title claims abstract description 47
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- 238000005057 refrigeration Methods 0.000 title claims abstract description 10
- 238000010992 reflux Methods 0.000 title abstract description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 67
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 238000000034 method Methods 0.000 claims abstract description 20
- 239000000284 extract Substances 0.000 claims description 18
- 229920006395 saturated elastomer Polymers 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 241000282326 Felis catus Species 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 239000005329 float glass Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OLBVUFHMDRJKTK-UHFFFAOYSA-N [N].[O] Chemical compound [N].[O] OLBVUFHMDRJKTK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001272 nitrous oxide Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
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Abstract
The invention provides a method for producing low purity oxygen with pressure and high purity nitrogen with pressure by adopting reflux expansion refrigeration. The method adopts a double-tower method to produce nitrogen and oxygen. The low purity liquid oxygen is pressurized by liquid level difference and is vaporized in a liquid oxygen evaporator and thereafter is discharged from a refrigerated box. According to the invention, rotating devices such as an oxygen compressor or a liquid oxygen pump or the like are avoided; equipment investment can be saved; energy consumption can be reduced; and added value of a product can be improved.
Description
Technical field
The present invention relates to a kind ofly carry out gas separation method, relate in particular to a kind of method of from air, separating low purity oxygen and high purity nitrogen through liquefaction.
Background technology
Along with the fast development of industries such as float glass, chemical industry, high pure nitrogen, band are forced down the pure oxygen demand and sharply increase, the float glass industry is 0.2 ~ 0.5MPa at the high pure nitrogen pressure that uses usually, nitrogen gas purity is 99.999% (O
2Concentration≤3ppm); Because the thawing of frit needs air or oxygen combustion-supporting, and along with the enforcement of national energy-saving and emission-reduction policy and the rising of fuel cost, comburant oxygen has more wide application prospect.Adopt comburant oxygen can significantly reduce nitrous oxide, emission of carbon-dioxide, and can fuel savings, improve the glass product grade, wherein the oxygen purity that needs of comburant oxygen preferably can be greater than 93% greater than 90%, pressure should be greater than 0.15MPa simultaneously.
Therefore airborne main gas componant is nitrogen and oxygen, and nitrogen and oxygen volume fraction are respectively 78.12% and 20.98%, and air is ubiquitous as low-cost resource, produces nitrogen through separation of air and oxygen is the most traditional method.
The 93%O that traditional low purity oxygen is empty to divide the double tower sky branch flow process that adopts air to expand into to go up tower to produce
2The equipment oxygen of lower purity oxygen extracts and can reach more than 99%, and single (general nitrogen pressure＜0.05MPa, oxygen＜0.07MPa), its power consumption is generally 0.5～0.55KWh/m because of oxygen, nitrogen pressure are low
3, energy consumption is higher, and its byproduct low-pressure nitrogen can not directly be carried, and needing increases nitrogen compressor, and nitrogen gas purity can not satisfy the demand of high-end float glass.The oxygen pressure of producing simultaneously is less than 0.1MPa, and float glass, chemical industry need high pure nitrogen, the lower purity oxygen of a large amount of band pressure, and nitrogen and oxygen pressure require greater than 0.15MPa.In order to reach the requirement of energy-saving and emission-reduction, high purity nitrogen, the low purity oxygen of Direct Production high extraction, band pressure are to have very much value from air separation process simultaneously.
All-oxygen combustion floatation glass production line, oxygen demand are far longer than the nitrogen demand, and oxygen nitrogen ratio is generally 3:1～4:1, so how air separation plant produces lower purity oxygen with pressure at low cost and a small amount of band presses nitrogen to become key.
Summary of the invention
The invention provides a kind of method of forcing down pure oxygen and high purity nitrogen with the air for the raw material production band; The double tower system of employing nitrogen system oxygen; Low pure liquid oxygen is vaporized with ice chest after through the liquid level difference supercharging in the liquid oxygen evaporimeter; Moving equipment such as oxygen compressor of avoiding or liquid oxygen pump have been saved equipment investment, have reduced energy consumption, have been improved added value of product.
To achieve these goals, the present invention provides a kind of stream backed expansion refrigeration production band to force down the method for pure oxygen and high purity nitrogen, comprises the steps:
The air of purifying, drying is cooled to saturation state, and a part of saturated air gets into Tata still down, and another part saturated air gets into the liquid oxygen evaporator condensation and becomes liquid air, and Tata still and saturated air separated into nitrogen and liquid air under liquid air got into; The nitrogen that following tower is separated is sent into tower,, be back to down top of tower then through condenser/evaporator nitrogen condensation becoming liquid nitrogen; Isolated liquia air gets into tower respectively and carries out rectifying in the liquid nitrogen that is back to down tower and the following tower, separates into the dirty nitrogen of band pressure and hangs down pure liquid oxygen.
Extract dirty nitrogen out from last tower middle and upper part, export through re-heat, after being expanded to atmospheric pressure; Extract high purity nitrogen from last top of tower, export after the re-heat; Low pure liquid oxygen is extracted out from last tower bottom and is got into the liquid oxygen evaporimeter; Between liquid oxygen evaporimeter and last tower bottom, exist under the action of pressure, liquid oxygen flashes to gas oxygen, exports through after the re-heat.
Other a kind of stream backed expansion refrigeration production band provided by the invention forces down the method for pure oxygen and high purity nitrogen, comprises the steps:
The air of purifying, drying is cooled to saturation state, and a part of saturated air gets into Tata still down, and another part saturated air gets into the liquid oxygen evaporator condensation and becomes liquid air, and Tata still and saturated air separated into nitrogen and liquid air under liquid air got into; The nitrogen that following tower is separated is sent into tower,, be back to down top of tower then through condenser/evaporator nitrogen condensation becoming liquid nitrogen; Isolated liquia air gets into tower respectively and carries out rectifying in the liquid nitrogen that is back to down tower and the following tower, separates into the dirty nitrogen of band pressure and hangs down pure liquid oxygen.
Extract dirty nitrogen out from last top of tower, export after being expanded to atmospheric pressure through re-heat, the machine that expands; Extract high purity nitrogen from following top of tower, export after the re-heat; Low pure liquid oxygen is extracted out from last tower bottom, gets into the liquid oxygen evaporimeter; Between liquid oxygen evaporimeter and last tower bottom, exist under the action of pressure, liquid oxygen flashes to gas oxygen, exports after the entering re-heat.
In the preferred embodiment in the present invention, the said operating pressure of going up tower is greater than 0.08MPa.
In the preferred embodiment in the present invention, said gas oxygen goes out pressure behind the main heat exchanger greater than 0.15MPa.
In the preferred embodiment in the present invention, said dirty nitrogen leaves after turbo-expander is expanded to atmospheric pressure.
In the preferred embodiment in the present invention, the difference in height between said condenser/evaporator and the liquid oxygen evaporimeter is greater than 5m.
In the preferred embodiment in the present invention, said condenser/evaporator, Shang Ta and following tower are integral structure, and condenser/evaporator is arranged on down top of tower, and condenser overhead is provided with tower.
In the preferred embodiment in the present invention, the number of plates of following tower is 50 ~ 100, and operating pressure is 0.6 ~ 1.1MPa.The number of plates of last tower is 40 ~ 100, and operating pressure is 0.08 ~ 0.25MPa.
The present invention compares with conventional art and has the following advantages:
1) the present invention adopts the raising upper tower pressure; Low pure liquid oxygen relies on gravity self-pressurization production band to press oxygen, and can produce band simultaneously and press high purity nitrogen, and the device cold is expanded by returning polluted nitrogen to be provided; Adopt air to expand with traditional low pure liquid oxygen from the supercharging flow process and into go up the tower ratio; All air get into upward tower rectifying separation after all having got into time tower rectifying, have improved the oxygen recovery rate, reach simultaneously and produce the purpose that band is pressed nitrogen.
2) nitrogen pressure of the present invention's production can reach 0.06 ~ 0.25MPa, and purity reaches 99.999% (oxygen content is less than 5ppm), and the oxygen purity of producing simultaneously can reach 90% ~ 98%, and pressure reaches 0.1 ~ 0.25MPa; And can extract the high-pressure nitrogen of oxygen output below 50% from following tower, and the oxygen recovery rate does not have obvious reduction, satisfies the required oxygen of float glass all-oxygen combustion, nitrogen simultaneously, does not need equipment such as extra oxygen, nitrogen compressor or liquid oxygen pump.
Description of drawings
Fig. 1 is the flow chart of the embodiment of the invention 1.
Fig. 2 is the flow chart of the embodiment of the invention 2.
Wherein, C1 is following tower, and C2 is last tower, and E1 is a main heat exchanger, and E2 is a subcooler, and K1 is last tower condenser/evaporator, and K2 is the liquid oxygen evaporimeter, and TP is a turbo-expander, and V1, V2, V3, V4 are choke valve.1,2,3 is compressed air, and 4 is liquid air, and 5 is liquid air, and 6 is post-decompression liquid air; 7 is liquid nitrogen, and 8 is the high-purity liquid nitrogen product, and 9 is post-decompression liquid nitrogen, and 10 is that last cat head band is pressed nitrogen; 11 are band pressure nitrogen product, and 12 is dirty nitrogen, and 13 are the dirty nitrogen before expanding, and 14 are the dirty nitrogen after the expansion; 15 is the dirty nitrogen of cooling box, and 16 are low pure liquid oxygen, and 17 bands for evaporation force down pure oxygen; 18 is that band forces down pure oxygen, and 19 is that the cat head band is pressed nitrogen down, and 20 is cooling box band pressure nitrogen product.
The specific embodiment
Stream backed expansion refrigeration production band provided by the invention forces down in the device of pure oxygen and high purity nitrogen; Adopt Xia Ta, go up the design of tower double tower; Different according to required nitrogen and oxygen purity and pressure; The number of plates and operating pressure can be selected from following scope respectively in the tower: following Tata plate quantity is 50 ~ 100, and operating pressure is at 0.6MPa ~ 1.1MPa; Last Tata plate quantity is 40 ~ 100, and operating pressure is at 0.08MPa ~ 0.25MPa.
Below through embodiment production band provided by the invention is forced down the method for pure oxygen and high purity nitrogen so that better understand the content of the invention, but the content of embodiment does not limit the protection domain of the invention.
With reference to Fig. 1, last tower C2 is connected through pipeline according to Fig. 1 mode with following tower C1, wherein, 45 blocks of column plates, operating pressure 0.12MPa is installed in the last tower C2; 50 blocks of column plates, operating pressure 0.65MPa are installed in the following tower C1.
The air 1 of removing carbon dioxide and water through molecular sieve adsorption cools off through main heat exchanger E1 and becomes saturation state; Part air 2 is sent into down among the tower C1; Part air 3 is sent into and is condensed into the liquid air 4 entering position of the above 3 blocks of column plates of tower bottom down among the liquid oxygen evaporimeter K2; The air of tower and the liquid nitrogen rectifying of liquid air and overhead reflux under getting into, cat head obtains nitrogen and the tower still obtains oxygen-rich liquid air 5.
The condenser/evaporator K1 of following tower nitrogen in last tower is cooled to the liquid nitrogen major part and is back to tower C1 down; Part liquid nitrogen 7 crossed through subcooler E2 send into the top of tower C2 through choke valve V3 after cold; Carry out rectifying; Liquid air 5 is gone up the 24th column plate place, tower top through choke valve V2 and is got into and go up tower and carry out rectifying, obtains nitrogen and low pure liquid oxygen with pressure, extracts nitrogen 10 out from cat head; Through subcooler E2 and main heat exchanger E1 re-heat, obtain the high pure nitrogen that supplies the user to use greater than 99.999% purity, 0.09MPa pressure.
Extract from last tower bottom that purity is 93%, pressure is the low pure liquid oxygen 16 of 0.13MPa out, through low pure liquid oxygen pipeline entering liquid oxygen evaporimeter.Because last tower condenser/evaporator top is than the high 7m that surpasses in liquid oxygen evaporimeter top; The difference in height of tower condenser/evaporator and liquid oxygen evaporimeter in the utilization; Increase liquid oxygen pressure 0.08MPa to 0.21MPa, evaporation in the liquid oxygen evaporimeter is after cooling box pressure >=0.17MPa after the main heat exchanger re-heat.
Extract nitrogen 10 from last top of tower position out, press nitrogen product 11 outputs as band through subcooler E2, main heat exchanger E1 re-heat to normal temperature.
Extract dirty nitrogen 12 out from 15 column plate positions, last tower top, re-heat gets into to-140 ℃～-160 ℃ and is expanded to atmospheric pressure among the turbo-expander TP or near the atmospheric pressure refrigeration, with the supplementary device cold in subcooler E2, main heat exchanger E1 hypomere.
With reference to Fig. 2, last tower C2 is connected through pipeline according to Fig. 2 mode with following tower C1, wherein, 40 blocks of column plates, operating pressure 0.11MPa is installed in the last tower C2; 55 blocks of column plates, operating pressure 0.62MPa are installed in the following tower C1.
The air 1 of removing carbon dioxide and water through molecular sieve adsorption cools off through main heat exchanger E1 and becomes saturation state; Part air 2 is sent into down among the tower C1; Part air 3 is sent into and is condensed into the liquid air 4 entering position of the above 3 blocks of column plates of tower bottom down among the liquid oxygen evaporimeter K2; The air of tower and the liquid nitrogen rectifying of liquid air and overhead reflux under getting into, cat head obtains nitrogen and the tower still obtains oxygen-rich liquid air 5.Extract pressure nitrogen gas 19 out from following column overhead,, obtain the pressure high pure nitrogen that supplies the user to use greater than 99.999% purity, 0.6MPa through main heat exchanger E1 re-heat cooling box.
The condenser/evaporator K1 of following tower nitrogen in last tower is cooled to the liquid nitrogen major part and is back to tower C1 down; Part liquid nitrogen 7 crossed through subcooler E2 send into the top of tower C2 through choke valve V3 after cold; Carry out rectifying; Liquid air 5 is gone up the 24th column plate place, tower top through choke valve V2 and is got into and go up tower and carry out rectifying, obtains nitrogen and low pure liquid oxygen with pressure.
Extract from last tower bottom that purity is 93%, pressure is the low pure liquid oxygen 16 of 0.11MPa out, through low pure liquid oxygen pipeline entering liquid oxygen evaporimeter.Because last tower condenser/evaporator top is than the high 7m that surpasses in liquid oxygen evaporimeter top; The difference in height of tower condenser/evaporator and liquid oxygen evaporimeter in the utilization; Increase liquid oxygen pressure 0.08MPa to 0.19MPa, evaporation in the liquid oxygen evaporimeter is after cooling box pressure >=0.15MPa after the main heat exchanger re-heat.
Extract dirty nitrogen 12 out from last top of tower or middle and upper part, re-heat gets into to-140 ℃ ~-160 ℃ and is expanded to atmospheric pressure among the turbo-expander TP or near the atmospheric pressure refrigeration, with the supplementary device cold in subcooler E2, main heat exchanger E1 hypomere.
In embodiment 1, make purity greater than 99.999%, pressure is the nitrogen of 0.09MPa, makes purity and be 93%, pressure is the oxygen of 0.17MPa.In embodiment 2, make purity greater than 99.999%, pressure is the nitrogen of 0.6MPa, makes purity and be 93%, pressure is the oxygen of 0.15MPa.
More than specific embodiment of the present invention is described in detail, but it is just as example, the present invention is not restricted to the specific embodiment of above description.To those skilled in the art, any equivalent modifications that the present invention is carried out with substitute also all among category of the present invention, also can look like embodiment 2 like enforcement mode 1 and extract pressure nitrogen gas at tower down, get into the main heat exchanger re-heat and export as product.Therefore, not breaking away from impartial conversion and the modification of being done under the spirit and scope of the present invention, all should contain within the scope of the invention.
Claims (9)
1. a stream backed expansion refrigeration production band forces down the method for pure oxygen and high purity nitrogen, it is characterized in that, comprises the steps:
The air of purifying, drying is cooled to saturation state, and a part of saturated air gets into Tata still down, and another part saturated air gets into the liquid oxygen evaporator condensation and becomes liquid air, and Tata still and saturated air separated into nitrogen and liquid air under liquid air got into; The nitrogen that following tower is separated is sent into tower,, be back to down top of tower then through condenser/evaporator nitrogen condensation becoming liquid nitrogen; Isolated liquia air gets into tower respectively and carries out rectifying in the liquid nitrogen that is back to down tower and the following tower, separates into the dirty nitrogen of band pressure and hangs down pure liquid oxygen;
Extract dirty nitrogen out from last tower middle and upper part, export through re-heat, after being expanded to atmospheric pressure; Extract high purity nitrogen from last top of tower, export after the re-heat; Low pure liquid oxygen is extracted out from last tower bottom and is got into the liquid oxygen evaporimeter; Between liquid oxygen evaporimeter and last tower bottom, exist under the action of pressure, liquid oxygen flashes to gas oxygen, exports through after the re-heat.
2. a stream backed expansion refrigeration production band forces down the method for pure oxygen and high purity nitrogen, it is characterized in that, comprises the steps:
The air of purifying, drying is cooled to saturation state, and a part of saturated air gets into Tata still down, and another part saturated air gets into the liquid oxygen evaporator condensation and becomes liquid air, and Tata still and saturated air separated into nitrogen and liquid air under liquid air got into; The nitrogen that following tower is separated is sent into tower,, be back to down top of tower then through condenser/evaporator nitrogen condensation becoming liquid nitrogen; Isolated liquia air gets into tower respectively and carries out rectifying in the liquid nitrogen that is back to down tower and the following tower, separates into the dirty nitrogen of band pressure and hangs down pure liquid oxygen;
Extract dirty nitrogen out from last top of tower, export after being expanded to atmospheric pressure through re-heat, the machine that expands; Extract high purity nitrogen from following top of tower, export after the re-heat;
Low pure liquid oxygen is extracted out from last tower bottom, gets into the liquid oxygen evaporimeter; Between liquid oxygen evaporimeter and last tower bottom, exist under the action of pressure, liquid oxygen flashes to gas oxygen, exports after the entering re-heat.
3. method according to claim 1 and 2 is characterized in that, the said operating pressure of going up tower is greater than 0.08MPa.
4. method according to claim 1 and 2 is characterized in that, said gas oxygen goes out pressure behind the main heat exchanger greater than 0.15MPa.
5. method according to claim 1 and 2 is characterized in that, said dirty nitrogen leaves after turbo-expander is expanded to atmospheric pressure.
6. method according to claim 1 and 2 is characterized in that, said condenser/evaporator top is higher than liquid oxygen evaporimeter top, and the difference in height between condenser/evaporator and the liquid oxygen evaporimeter is greater than 5m.
7. method according to claim 1 and 2 is characterized in that, said condenser/evaporator, Shang Ta and following tower are integral structure, and condenser/evaporator is arranged on down top of tower, and condenser overhead is provided with tower.
8. method according to claim 1 and 2 is characterized in that, the said number of plates of tower down is 50 ~ 100, and operating pressure is 0.6 ~ 1.1MPa.
9. method according to claim 1 and 2 is characterized in that, the said number of plates that goes up tower is 40 ~ 100, and operating pressure is 0.08 ~ 0.25MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210125303.7A CN102721261B (en) | 2012-04-26 | 2012-04-26 | Method for producing low purity oxygen with pressure and high purity nitrogen with pressure by adopting reflux expansion refrigeration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210125303.7A CN102721261B (en) | 2012-04-26 | 2012-04-26 | Method for producing low purity oxygen with pressure and high purity nitrogen with pressure by adopting reflux expansion refrigeration |
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| Publication Number | Publication Date |
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| CN102721261A true CN102721261A (en) | 2012-10-10 |
| CN102721261B CN102721261B (en) | 2014-11-05 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103759500A (en) * | 2014-01-24 | 2014-04-30 | 浙江大川空分设备有限公司 | Method and device for manufacturing high purity nitrogen in low energy consumption mode |
| CN112066645A (en) * | 2020-09-25 | 2020-12-11 | 杭州贝斯特气体有限公司 | Pressure Oxygen Production System |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5410885A (en) * | 1993-08-09 | 1995-05-02 | Smolarek; James | Cryogenic rectification system for lower pressure operation |
| CN101886871A (en) * | 2010-08-04 | 2010-11-17 | 四川空分设备(集团)有限责任公司 | Method and device for producing pressure oxygen by air separation |
| CN102230716A (en) * | 2011-06-08 | 2011-11-02 | 杭州优埃基空分设备有限公司 | Method and device for separating air through air pressurization, backflow expansion and internal compression |
-
2012
- 2012-04-26 CN CN201210125303.7A patent/CN102721261B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5410885A (en) * | 1993-08-09 | 1995-05-02 | Smolarek; James | Cryogenic rectification system for lower pressure operation |
| CN101886871A (en) * | 2010-08-04 | 2010-11-17 | 四川空分设备(集团)有限责任公司 | Method and device for producing pressure oxygen by air separation |
| CN102230716A (en) * | 2011-06-08 | 2011-11-02 | 杭州优埃基空分设备有限公司 | Method and device for separating air through air pressurization, backflow expansion and internal compression |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103759500A (en) * | 2014-01-24 | 2014-04-30 | 浙江大川空分设备有限公司 | Method and device for manufacturing high purity nitrogen in low energy consumption mode |
| CN112066645A (en) * | 2020-09-25 | 2020-12-11 | 杭州贝斯特气体有限公司 | Pressure Oxygen Production System |
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| CN102721261B (en) | 2014-11-05 |
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Effective date of registration: 20210705 Address after: 201800 rooms 202 and 204, building 3, 150 Heyu Road, Jiading District, Shanghai Patentee after: SHANGHAI QIYUAN GAS DEVELOPMENT Co.,Ltd. Address before: No.150 Heyu Road, Jiading District, Shanghai, 201802 Patentee before: SHANGHAI QIYUAN AIR SEPARATE TECHNOLOGY DEVELOPMENT Co.,Ltd. |
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