CN201729660U - Oxygen generator set - Google Patents
Oxygen generator set Download PDFInfo
- Publication number
- CN201729660U CN201729660U CN2010202594904U CN201020259490U CN201729660U CN 201729660 U CN201729660 U CN 201729660U CN 2010202594904 U CN2010202594904 U CN 2010202594904U CN 201020259490 U CN201020259490 U CN 201020259490U CN 201729660 U CN201729660 U CN 201729660U
- Authority
- CN
- China
- Prior art keywords
- argon
- oxygenerator
- crude
- pure
- crude argon
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Abstract
The utility model provides an oxygen generator set which is characterized in that one hydrogenation argon and oxygen generator and one hydrogen-free argon and oxygen generator, at least two hydrogen-free argon and oxygen generators or at least two hydrogenation argon and oxygen generators are connected in a combining way through a liquid pipeline, a gas pipeline, a liquid storage device and a gas storage device, and crude argon which is not hydrogenated and deoxidized or crude argon which is liquefied and denitrogenated in one hydrogenation argon and oxygen generator is input into the crude argon tower of the hydrogen-free argon and oxygen generator for secondary deoxidization and into the pure argon tower of the hydrogen-free argon and oxygen generator for denitrogenation to obtain pure liquid argon, or is input into the other hydrogenation argon and oxygen generator for joint compression, is introduced into a crude argon purifier for hydrogenation and deoxidization, is cooled through heat exchange by a plate heat exchanger and is input into the pure argon tower for nitrogen and argon separation to obtain pure liquid argon. The utility model has the advantages that at least one hydrogen generation station can be saved, the oxygen generator set is suitable for the reconstruction of the existing hydrogenation argon and oxygen generators and the hydrogen-free argon and oxygen generators, the argon yield of the oxygen generator is improved and the argon generation cost is reduced.
Description
Technical field
The utility model relates to the gas producing apparatus, particularly a kind of oxygenerator group.
Background technology
The oxygenerator that has argon making process can be divided into two kinds of the oxygenerators of the oxygenerator of hydrogenation argon making process and hydrogen-free argon producing flow process on the technology.The oxygenerator of hydrogenation argon making process is domestic oxygenerator fourth, fifth generation product, and its structure is generally the sieve-tray tower structure; And the oxygenerator of hydrogen-free argon producing flow process be the 6th generation product, technology advanced person is the packing tower structure.This product of two types also is the present domestic product that is most widely used.
With regard to hydrogenation system argon oxygenerator, because the electrolyzer current consumption of supporting hydrogen producer is big, the electricity charge in 1 year can reach (electrolyzer power consumption size is relevant with hydrogen manufacturing amount size) more than 600,000 yuan, and the hydrogen manufacturing safety coefficient is low, very easily blast, so a lot of enterprises all leave unused this part function get off, and have wasted the argon resource of oxygenerator.Though and the hydrogen-free argon producing oxygenerator does not have this problem, find in the use that the design discharge of crude argon is on the low side, and the argon fraction to contain the argon rate limited, the equipment that makes fails to give full play to its throughput.
The utility model content
At the problems referred to above, the utility model provides a kind of oxygenerator group, the combination of the hydrogenation system of utilization argon oxygenerator and hydrogen-free argon producing oxygenerator, thick liquid argon after crude argon that hydrogenation system argon oxygenerator is produced or liquefaction are denitrogenated is introduced the hydrogen-free argon producing oxygenerator, participation rectifying is extracted, and can improve the argon output of oxygenerator.
The utility model also provides a kind of oxygenerator group, with two or more hydrogenation system argon oxygenerator combinations, without the crude argon of deoxidization by adding hydrogen, introduce tail end hydrogenation system argon oxygenerator and cause deoxygenation in the argon purifier, be that the pure argon column that low temperature enters tail end hydrogenation oxygenerator carries out nitrogen, the argon separation obtains pure liquid argon in the argon making process of front end hydrogenation system argon oxygenerator through the plate-type heat exchanger heat exchange through common compression.Thereby the minimizing hydrogen generator station, the reduction expense.
The technical scheme that its technical problem that solves the utility model adopts is:
A kind of oxygenerator group comprises first oxygenerator with hydrogenation argon making process and second oxygenerator with hydrogen-free argon producing flow process,
Thick liquid argon after the denitrogenating without the crude argon of deoxidization by adding hydrogen or liquefaction of described first oxygenerator output inputs to crude argon two towers of described second oxygenerator by the liquids and gases pipeline;
Oxygen, argon separate crude argon condenser that the crude argon that obtains inputs to described second oxygenerator and carry out the liquefaction of heat exchange condensation portion and reflux for the second time by crude argon two towers of described second oxygenerator;
The pure argon column that inputs to described second oxygenerator from the thick gas argon of the low temperature that do not liquefy of the crude argon condenser of described second oxygenerator output carries out rectifying and realizes that nitrogen, argon separate, and by the pure liquid argon of pure argon column bottom output of described second oxygenerator.
Preferably, further comprise the liquids and gases storing unit in the described liquids and gases pipeline.
A kind of oxygenerator group also is provided, has comprised at least two first oxygenerators that are linked in sequence with hydrogenation argon making process,
Thick gas argon from described first oxygenerator output that is positioned at front end without deoxidization by adding hydrogen, input to by gas pipeline the first oxygenerator crude argon compressor that is positioned at the rear end the suction side, thick gas argon with described first oxygenerator that is positioned at the rear end inputs to argon purifier after common compression, carry out drying and cooling;
Input to the described pure argon column that is positioned at first oxygenerator of rear end by the thick gas argon of the argon purifier output of described first oxygenerator that is positioned at the rear end and carry out rectifying and denitrogenate, and the thick liquid argon after denitrogenating by the described pure argon column bottom output that is positioned at first oxygenerator of rear end.
Preferably, further comprise the liquids and gases storing unit in the described liquids and gases pipeline.
Preferably, described oxygenerator group further comprises second oxygenerator with hydrogen-free argon producing flow process,
From described thick liquid argon after being positioned at front end and being positioned at the denitrogenating of rear end first oxygenerator output, input to crude argon two towers of described second oxygenerator and the crude argon of described second oxygenerator converges by the second liquids and gases pipeline without the crude argon of deoxidization by adding hydrogen or liquefaction;
Oxygen, argon separate that the crude argon two tower condenser portion liquefaction that the crude argon that obtains inputs to described second oxygenerator refluxes, the part low temperature crude argon output of not liquefaction for the second time by crude argon two towers of described second oxygenerator;
The pure argon column that inputs to described second oxygenerator from the low temperature crude argon of the crude argon condenser of described second oxygenerator output carries out rectifying and realizes that nitrogen, argon separate, and by the pure liquid argon of pure argon column bottom output of described second oxygenerator.
Preferably, further comprise the argon liquefier,
The pure argon column that inputs to described second oxygenerator from the low temperature crude argon (or without liquefaction directly) after described argon liquefier liquefaction that the crude argon condenser of described second oxygenerator is exported carries out rectifying.
The utility model also provides a kind of oxygenerator group, comprise at least two second oxygenerators that are linked in sequence with hydrogen-free argon producing flow process, the defective thick liquid argon that contains oxygen 〉=10PPm from the described second oxygenerator pure argon column output that is positioned at front end, crude argon two towers that input to described second oxygenerator that is positioned at the rear end by fluid pipeline carry out the rectifying deoxygenation
The thick liquid argon that oxygen 〉=10PPm does not denitrogenate that contains from the argon liquefier bottom output of described second oxygenerator that is positioned at front end inputs to described crude argon two tower bottoms that are positioned at second oxygenerator of rear end by fluid pipeline and carries out the rectifying deoxygenation,
Input to the described pure argon column that is positioned at second oxygenerator of rear end by the crude argon that contains oxygen＜10PPm, do not denitrogenate of the described second oxygenerator crude argon, the two towers output that is positioned at the rear end and carry out rectifying and denitrogenate, and by the pure liquid argon of second oxygenerator pure argon column bottom output.
Preferably, further comprise liquid storaging device and liquid pressurizing device in the described fluid pipeline.
Preferably, described fluid pipeline can with the described arbitrary crude argon pipe connection that is positioned at the second oxygenerator crude argon, two towers of front end.
By above technical scheme as can be known, oxygenerator group of the present utility model, by with hydrogenation system argon oxygenerator and hydrogen-free argon producing oxygenerator or at least two hydrogenation system argon oxygenerators, be connected by liquid, gas pipeline and liquid, reserve of gas device, crude argon after denitrogenating without the crude argon of deoxidization by adding hydrogen or liquefaction in the hydrogenation system of the making argon oxygenerator, the argon purifier that inputs to hydrogen-free argon producing oxygenerator or another hydrogenation system argon oxygenerator carries out deoxidization by adding hydrogen, and after further denitrogenating purification, obtain pure liquid argon to pure argon column rectifying.The utility model can be saved a hydrogen generator station at least, is applicable to the transformation to existing hydrogenation system argon oxygenerator and hydrogen-free argon producing oxygenerator, and the argon output of oxygenerator is provided, and reduces system argon cost.
Description of drawings
Fig. 1 is the structural representation of first embodiment of oxygenerator group of the present utility model.
Fig. 2 is the structural representation of second embodiment of oxygenerator group of the present utility model.
Fig. 3 is the structural representation of the 3rd embodiment of oxygenerator group of the present utility model.
Embodiment
The purpose of this utility model is to provide a kind of oxygenerator group, the combination of the hydrogenation system of utilization argon oxygenerator and hydrogen-free argon producing oxygenerator, the perhaps combination of two and two above hydrogenation system argon oxygenerators, the crude argon that bleeds off in vain in the hydrogenation system argon oxygenerator is carried out oxygen, argon separation, and further rectifying is extracted, thereby obtain pure liquid argon, can improve the argon output of oxygenerator, and save at least one hydrogen generator station.
For making the purpose of this utility model, technical scheme and advantage clearer, below with reference to the accompanying drawing embodiment that develops simultaneously, the utility model is further described.
Fig. 1 is the structural representation of first embodiment of oxygenerator group of the present utility model.As shown in Figure 1, oxygenerator group of the present utility model comprises first oxygenerator 101 with hydrogenation argon making process and second oxygenerator 102 with hydrogen-free argon producing flow process.
Tower 5 from the separation column of first oxygenerator 101, with 8～12%, nitrogen content is less than 0.06% argon fraction gas, input to crude argon column 3 by managing 1, fraction after condenser 4 liquefaction is got back to tower 5 on the separation column through managing 2, while argon fraction contains the crude argon of argon 〉=98% from managing 6 outputs through the rectifying simmer down to, enter 7 compressions of argon gas compressor.
Wherein the intake pressure of argon gas compressor 7 is 〉=0.001MPa, and exhaust pressure is 〉=0.13MPa.
Crude argon through 7 compressions of argon gas compressor enters the waste gas heat exchange that process argon interchanger and low wet nitrogen and pure argon column are discharged, enter pure argon column 8 bottommost process argon containers, with be condensed into liquid after the pure liquid argon heat exchange in heat exchange of technology nitrogen and the pure argon column 8, condensed thick liquid argon is exported from pure argon column bottommost process argon container bottom, enter pure argon column 8 and participate in rectifying, nitrogen component separation in the liquid argon is discharged as waste gas from smart argon condenser overhead, the higher gas argon of purity is got back to crude argon column 8 bottoms again from smart argon condenser condenses, thereby obtains denitrogenating the liquid argon work in-process of back content≤3% oxygen in pure argon column 8 bottoms.
Liquid argon work in-process after the liquefaction of first oxygenerator 101 output is denitrogenated or without deoxidization by adding hydrogen, the crude argon denitrogenated, input to crude argon column 11 bottoms of second oxygenerator 102 by liquids and gases pipeline 10, crude argon with the crude argon column 12 of second oxygenerator 102 carries out the rectifying deoxygenation at crude argon column 11 jointly.
By crude argon column 11 for the second time oxygen, argon separate the crude argon condenser 13 that the crude argon that obtains inputs to second oxygenerator 102 and carry out the heat exchange condensation, partial condensation liquefaction is as the phegma of crude argon column 11, liquefaction does not contain the low temperature crude argon of oxygen≤10ppm.Thick liquid argon is back to crude argon column 11 through pipeline 14, and crude argon imports liquefier 16 liquefaction (or directly entering pure argon column) through pipeline 15.
Input to pure argon column 18 from the liquid argon of crude argon liquefier 16 output through pipeline and carry out rectifying and denitrogenate, and export pure liquid argon by pure argon column 18 bottoms.
Preferably, can further comprise in the liquids and gases pipeline 10 and be used to store thick liquid argon and crude argon liquids and gases storing unit.
Fig. 2 is the structural representation of the another kind of embodiment of oxygenerator group of the present utility model.As shown in Figure 2, oxygenerator group of the present utility model comprises first oxygenerator 201 and 202 with the hydrogenation argon making process that is linked in sequence, and the oxygen flow that wherein is positioned at first oxygenerator 201 of front end is 〉=2000m
3/ h, the oxygen flow that is positioned at first oxygenerator 202 of rear end is 〉=3000m
3/ h.
From the crude argon or the liquid argon without deoxidization by adding hydrogen of first oxygenerator 201 output, input to the crude argon compressor suction side of first oxygenerator 202 by gas pipeline;
By the crude argon column of first oxygenerator 202 for the first time oxygen, argon separate the crude argon input crude argon compressor suction side that obtains, compress jointly with rough argon from the crude argon column of first oxygenerator 201.
To the argon purifier of first oxygenerator 202, carry out deoxygenation, condensation, drying and cooling;
The pure argon column that is inputed to first oxygenerator 202 by the rough argon of the argon purifier of first oxygenerator 202 output carries out rectifying, and by the pure liquid argon of pure argon column bottom output of first oxygenerator 202.
Preferably, can further comprise in the liquids and gases pipeline and be used to store thick liquid argon and crude argon liquids and gases storing unit.
Oxygenerator group of the present utility model can further comprise second oxygenerator 203 with hydrogen-free argon producing flow process.
After the crude argon discharge tube G-2 of the crude argon discharge tube G-1 of crude argon column 301 upper ends of first oxygenerator 201 and crude argon column 302 upper ends of first oxygenerator 202 joins, by the argon compressor compresses, the pure argon column 303 that enters first oxygenerator 202 along pipeline G-3 carries out rectifying, condensation, the liquid argon work in-process of gained are connected with the crude argon column 304 of second oxygenerator 203 through piping G-4, crude argon with crude argon column 304 gained of second oxygenerator 203, enter the crude argon column 305 of second oxygenerator 203 jointly, carry out oxygen, argon separates, part is carried out after the heat exchange condensation phegma as 305 through condenser, Ye Hua low temperature crude argon (does not contain oxygen≤10ppm) and enters argon liquefier liquefaction (or without liquefaction directly) and enter pure argon column 306 rectifying and remove nitrogen component in second oxygenerator, 203 crude argons, and obtain pure liquid argon in pure argon column 306 bottoms.
Fig. 3 is the structural representation of the 3rd embodiment of oxygenerator group of the present utility model.As shown in Figure 3, oxygenerator group of the present utility model comprises second oxygenerator 401 and 402 with the hydrogen-free argon producing flow process that is linked in sequence.
Contain the defective liquid argon of oxygen 〉=10ppm from the output of pure argon column 428 bottoms of second oxygenerator 401 that is positioned at front end, input to crude argon two towers 421 of second oxygenerator 402 that is positioned at the rear end by fluid pipeline 412, the crude argon that is produced with second oxygenerator 402 carries out the rectifying deoxygenation jointly
Oxygen 〉=the 10ppm that contains that exports from the described argon liquefier 426 that is positioned at second oxygenerator 401 of front end does not denitrogenate defective thick liquid argon, input to crude argon two towers 421 of second oxygenerator 402 that is positioned at the rear end by fluid pipeline 412, the crude argon that is produced with second oxygenerator 402 carries out the rectifying deoxygenation jointly
The pure argon column 423 that inputs to second oxygenerator 402 that is positioned at the rear end by the crude argon after the deoxygenation of crude argon two towers 421 output of second oxygenerator 402 that is positioned at the rear end carries out rectifying to be denitrogenated, and by the pure liquid argon of the pure argon column 423 bottoms output of second oxygenerator 402.
Preferably, can further comprise liquid storaging device and liquid pressurizing device in the fluid pipeline 412.
Preferably, fluid pipeline 412 can with crude argon one tower 424 of second oxygenerator 401 that is positioned at front end and the arbitrary thick liquid argon pipe connection of crude argon two towers 422.
From above scheme as can be known, oxygenerator group of the present utility model is by with hydrogenation system argon oxygenerator and hydrogen-free argon producing oxygenerator or at least two hydrogenation system argon oxygenerators, be connected by liquid, gas pipeline and liquid, reserve of gas device, in the hydrogenation system of the making argon oxygenerator without the crude argon of deoxidization by adding hydrogen or thick liquid argon, the crude argon column that inputs to hydrogen-free argon producing oxygenerator or another hydrogenation system argon oxygenerator carries out oxygen, argon separates, and after further rectification and purification is denitrogenated, obtain pure liquid argon.
The oxygenerator group of hydrogenation system argon oxygenerator of the present utility model and the combination of hydrogen-free argon producing oxygenerator can be saved the utility appliance of hydrogen generator station and the outer hydrogenation deoxidation of tower, and per tour can be reduced by at least two operative employees, reduces the cost and the power consumption of hydrogen manufacturing.In addition, do not need other hydrogenation, improved the security of system argon yet.The array mode of this oxygenerator is compared with unit production, has improved output, has shortened the production cycle, and operating mode recovers fast when maintenance and fault.
When a kind of oxygenerator group of two hydrogen-free argon producing oxygenerators combination of the present utility model broke down at any position of any oxygenerator, the production of an other oxygenerator can not be affected.Simultaneously, this oxygenerator group can (comprise all component equipments of ar system in the equipment failure of any oxygenerator ar system, as the argon column body, condenser, pipeline, valve, pump, instrument element) time, the equipment and the postorder oxygen generation system thereof that only need this oxygenerator of stoppage in transit to break down, simultaneously with the argon fraction gas of out of order oxygenerator, or crude argon, perhaps thick liquid argon is incorporated in another oxygenerator ar system relevant device in the oxygenerator group by gas or fluid pipeline, make originally because of the undrawn argon cut of ar system overhaul of the equipments gas, or crude argon obtains rectifying, purify and send with finished product, save the argon resource, increased economic benefit.In addition, when this oxygenerator group is recovered argon production after described second oxygenerator maintenance and handling failure, can in advance the thick liquid of first oxygenerator be introduced into the crude argon column of second oxygenerator, improve the second oxygenerator crude argon purity, fast quick-recovery argon operating mode.
A kind of oxygenerator group of two hydrogenation system argon oxygenerators combination of the present utility model can be saved a cover hydrogen generator station and be reduced the hydrogen manufacturing cost.In addition, when this oxygenerator group can be recovered argon production after described second oxygenerator maintenance and handling failure, liquid argon after can be in advance the crude argon of first oxygenerator or liquefaction being denitrogenated is introduced in the oxygen purifier of second oxygenerator and carries out deoxygenation, cooling and drying, and be delivered to the argon column of second oxygenerator, reach fast quick-recovery operating mode, send the purpose of argon in advance.The oxygenerator group of a plurality of hydrogenation system argon oxygenerator of the present utility model and the combination of hydrogen-free argon producing oxygenerator can be saved a hydrogen generator station at least, has saved cost greatly.
The above only is preferred embodiment of the present utility model; not in order to restriction the utility model; all within spirit of the present utility model and principle, any modification of being made, be equal to replacement, improvement etc., all should be included within the scope of the utility model protection.
Claims (9)
1. an oxygenerator group is characterized in that,
Comprise first oxygenerator with hydrogenation argon making process and second oxygenerator with hydrogen-free argon producing flow process,
Thick liquid argon after the denitrogenating without the crude argon of deoxidization by adding hydrogen or liquefaction of described first oxygenerator output inputs to crude argon two towers of described second oxygenerator by the liquids and gases pipeline;
Converge by crude argon two towers of described second oxygenerator and the crude argon of described second oxygenerator, carry out for the second time oxygen, argon and separate crude argon condenser that the crude argon that obtains inputs to described second oxygenerator and carry out the liquefaction of heat exchange condensation portion and reflux;
The pure argon column that inputs to described second oxygenerator from the thick gas argon of the low temperature that do not liquefy of the crude argon condenser of described second oxygenerator output carries out rectifying and realizes that nitrogen, argon separate, and by the pure liquid argon of pure argon column bottom output of described second oxygenerator.
2. oxygenerator group according to claim 1 is characterized in that, further comprises the liquids and gases storing unit in the described liquids and gases pipeline.
3. an oxygenerator group is characterized in that,
Comprise at least two first oxygenerators that are linked in sequence with hydrogenation argon making process,
Thick gas argon from described first oxygenerator output that is positioned at front end without deoxidization by adding hydrogen, input to by gas pipeline the first oxygenerator crude argon compressor that is positioned at the rear end the suction side, thick gas argon with described first oxygenerator that is positioned at front end inputs to argon purifier after common compression, carry out drying and cooling;
Input to the described pure argon column that is positioned at first oxygenerator of rear end by the thick gas argon of the argon purifier output of described first oxygenerator that is positioned at the rear end and carry out rectifying and denitrogenate, and the thick liquid argon after denitrogenating by the described pure argon column bottom output that is positioned at first oxygenerator of rear end.
4. oxygenerator group according to claim 3 is characterized in that, further comprises the liquids and gases storing unit in the described liquids and gases pipeline.
5. oxygenerator group according to claim 4 is characterized in that, described oxygenerator group further comprises second oxygenerator with hydrogen-free argon producing flow process,
From described thick liquid argon after being positioned at front end and being positioned at the denitrogenating of rear end first oxygenerator output, input to crude argon two towers of described second oxygenerator and the crude argon of described second oxygenerator converges by the second liquids and gases pipeline without the crude argon of deoxidization by adding hydrogen or liquefaction;
Crude argon two towers by described second oxygenerator carry out the oxygen second time, argon separates the crude argon two tower argon condensers that the crude argon that obtains inputs to described second oxygenerator, and partial liquefaction refluxes, the part low temperature crude argon output of not liquefaction;
The pure argon column that inputs to described second oxygenerator from the low temperature crude argon of the crude argon condenser of described second oxygenerator output carries out rectifying and realizes that nitrogen, argon separate, and by the pure liquid argon of pure argon column bottom output of described second oxygenerator.
6. oxygenerator group according to claim 5 is characterized in that, further comprises the argon liquefier,
The pure argon column that inputs to described second oxygenerator from the low temperature crude argon that the crude argon condenser of described second oxygenerator is exported after described argon liquefier liquefaction carries out rectifying.
7. an oxygenerator group is characterized in that,
Comprise at least two second oxygenerators that are linked in sequence with hydrogen-free argon producing flow process, the defective thick liquid argon that contains oxygen 〉=10PPm from the described second oxygenerator pure argon column output that is positioned at front end, crude argon two towers that input to described second oxygenerator that is positioned at the rear end by fluid pipeline carry out the rectifying deoxygenation
The thick liquid argon that oxygen 〉=10PPm does not denitrogenate that contains from the argon liquefier bottom output of described second oxygenerator that is positioned at front end inputs to described crude argon two towers that are positioned at second oxygenerator of rear end by fluid pipeline and carries out the rectifying deoxygenation,
Input to the described pure argon column that is positioned at second oxygenerator of rear end by the crude argon that contains oxygen＜10PPm, do not denitrogenate of the described second oxygenerator crude argon, the two towers output that is positioned at the rear end and carry out rectifying and denitrogenate, and by the pure liquid argon of second oxygenerator pure argon column bottom output.
8. oxygenerator group according to claim 7 is characterized in that, further comprises liquid storaging device and liquid pressurizing device in the described fluid pipeline.
9. oxygenerator group according to claim 7 is characterized in that, described fluid pipeline can with the described arbitrary crude argon pipe connection that is positioned at the second oxygenerator crude argon, two towers of front end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202594904U CN201729660U (en) | 2010-07-12 | 2010-07-12 | Oxygen generator set |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202594904U CN201729660U (en) | 2010-07-12 | 2010-07-12 | Oxygen generator set |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201729660U true CN201729660U (en) | 2011-02-02 |
Family
ID=43520816
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202594904U Expired - Fee Related CN201729660U (en) | 2010-07-12 | 2010-07-12 | Oxygen generator set |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201729660U (en) |
-
2010
- 2010-07-12 CN CN2010202594904U patent/CN201729660U/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202675796U (en) | Device utilizing liquefied Natural Gas (LNG) cold energy to produce liquid air separation products | |
| CN101723338A (en) | Method for extracting krypton-xenon from liquid oxygen | |
| CN203534058U (en) | Liquid argon storage groove gasified argon recovery device | |
| CN101886870A (en) | Method and device for producing pressure high-purity nitrogen and high-purity oxygen | |
| CN102030314B (en) | Oxygen generator | |
| CN106219495A (en) | A kind of small-sized PSA and the combination unit of small-sized cryogenic air separation unit | |
| CN109437234A (en) | A kind of compound semiconductor epitaxial tail gas recycling device and method | |
| CN202216490U (en) | Extraction device for high-purity liquid neon | |
| CN201729660U (en) | Oxygen generator set | |
| CN204718302U (en) | A kind of oxygen enrichment system of efficiency utilization LNG cold energy | |
| CN107297124A (en) | A kind of coproduction CO2Rectisol system and using its reclaim CO2Method | |
| CN114485051B (en) | Liquid ammonia double-working-condition refrigerating system and liquid carbon dioxide production equipment | |
| CN1325865C (en) | Method for producing argon with oxygenerator set | |
| CN102923731B (en) | Utilizing device and method for cold energy in high-purity ammonia preparation process | |
| CN204648831U (en) | Compression oxygenerator in a kind of single tower | |
| CN203615679U (en) | Single-tower oxygen generation device | |
| CN210892361U (en) | Device for preparing liquid carbon dioxide by utilizing surplus cold energy for refrigeration | |
| CN209306960U (en) | A kind of compound semiconductor epitaxial tail gas recycling device | |
| CN207751221U (en) | A kind of heat pump air-seperation system of LNG cold energy uses | |
| CN102829606B (en) | Air separation unit for preparing high-purity liquid nitrogen by utilizing liquid oxygen reladling | |
| CN209027187U (en) | A kind of peak-trough electricity production liquid oxygen liquid nitrogen plan | |
| CN206176891U (en) | Air separation device with high pressure heat transfer oxygen suppliment | |
| CN201413000Y (en) | Novel air separation device | |
| CN205027036U (en) | Carbon dioxide economizer | |
| CN207268560U (en) | Distributed photovoltaic power supply medical oxygen device for making |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110202 Termination date: 20180712 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |