CN1228128C - Variable pressure adsorptive oxygen making device suitable for high altitude area - Google Patents
Variable pressure adsorptive oxygen making device suitable for high altitude area Download PDFInfo
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- CN1228128C CN1228128C CN 200310122470 CN200310122470A CN1228128C CN 1228128 C CN1228128 C CN 1228128C CN 200310122470 CN200310122470 CN 200310122470 CN 200310122470 A CN200310122470 A CN 200310122470A CN 1228128 C CN1228128 C CN 1228128C
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- 239000001301 oxygen Substances 0.000 title claims abstract description 39
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 39
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 230000000274 adsorptive effect Effects 0.000 title description 10
- 238000001179 sorption measurement Methods 0.000 claims abstract description 161
- 239000007789 gas Substances 0.000 claims abstract description 106
- 238000000034 method Methods 0.000 claims abstract description 20
- 230000008569 process Effects 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 230000001105 regulatory effect Effects 0.000 claims abstract description 4
- 230000007613 environmental effect Effects 0.000 claims abstract 2
- 238000000926 separation method Methods 0.000 abstract description 7
- 238000010276 construction Methods 0.000 abstract description 3
- 230000029058 respiratory gaseous exchange Effects 0.000 abstract 1
- 238000010521 absorption reaction Methods 0.000 description 29
- 238000003795 desorption Methods 0.000 description 22
- 239000002808 molecular sieve Substances 0.000 description 16
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 16
- 230000006837 decompression Effects 0.000 description 10
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 230000009466 transformation Effects 0.000 description 6
- 239000010457 zeolite Substances 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 235000019628 coolness Nutrition 0.000 description 5
- 230000008878 coupling Effects 0.000 description 5
- 238000010168 coupling process Methods 0.000 description 5
- 238000005859 coupling reaction Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 5
- 238000011069 regeneration method Methods 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 3
- 230000006353 environmental stress Effects 0.000 description 3
- 238000011027 product recovery Methods 0.000 description 3
- 239000002594 sorbent Substances 0.000 description 3
- 101001064895 Epichloe festucae var. lolii D-lysergyl-peptide-synthetase subunit 1 Proteins 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
一种适于高海拔地区用的变压吸附制氧装置。本发明涉及空气分离领域的一种变压吸附制氧装置，该装置由无油空气压缩机、空气冷却器、吸附塔、产品气储气罐、气动阀门、减压阀、针型阀、流量计、流量调节阀等部件构成，其特征在于装置中设置了一个原料气储气罐3，原料气储气罐3的作用是稳定吸附床出口的压力，储存均压过程中的压缩机排气，减小产品气流量的波动以及环境压力对装置性能的影响。对于海拔超过4000米以上的地区，为保证系统正常运行，空气压缩机的排气压力为0.1～0.7Mpa，原料气储气罐的容积为吸附塔容积的1.1～3倍，所需的原料气源容量匹配为产品气量的21～50倍。本发明可以为高海拔地区的施工和工作人员提供呼吸和医疗保健用氧以及有关工业用氧，具有设备简单、调节方便、自动化程度高等优点。
A pressure swing adsorption oxygen generator suitable for use in high altitude areas. The invention relates to a pressure swing adsorption oxygen generator in the field of air separation. The device consists of an oil-free air compressor, an air cooler, an adsorption tower, a product gas storage tank, a pneumatic valve, a pressure reducing valve, a needle valve, a flow Meter, flow regulating valve and other components, characterized in that a raw material gas storage tank 3 is set in the device. The function of the raw material gas storage tank 3 is to stabilize the pressure at the outlet of the adsorption bed, and to store the exhaust gas of the compressor during the pressure equalization process. , to reduce the fluctuation of product gas flow and the influence of environmental pressure on the performance of the device. For areas with an altitude of more than 4000 meters, in order to ensure the normal operation of the system, the exhaust pressure of the air compressor is 0.1-0.7Mpa, and the volume of the raw gas storage tank is 1.1-3 times the volume of the adsorption tower. The matching source capacity is 21 to 50 times the gas volume of the product. The invention can provide oxygen for breathing, medical care and related industries for construction and workers in high-altitude areas, and has the advantages of simple equipment, convenient adjustment, high degree of automation, and the like.
Description
Technical field
The present invention relates to a kind of pressure swing adsorption oxygen making device in air separation field, be specially adapted to the high altitude localities.
Background technology
Pressure swing adsorption is proposed by people such as Skarstrom the earliest, its ultimate principle is to utilize the difference of different components equilibrium adsorption capacity, rate of diffusion on sorbent material in the mixed gas and adsorptive capacity to increase, reduce with pressure the characteristic that reduces with the pressure rising, under pressurized conditions, finish the adsorption separation process of mixed gas, the gaseous fraction desorb that is adsorbed under the pressure-lowering condition, adsorbent reactivation, thus the separation and the sorbent circulation of each component of realization mixed gas are used.Eighties of last century is since the eighties, and pressure swing adsorption has obtained using widely in the gas delivery industry.As sorbent material, utilizing the pressure-swing adsorption process separation of air can produce concentration is about 95% oxygen with zeolite molecular sieve.According to the difference of working pressure range, pressure-swing adsorption process can be divided into two kinds:
(1) PSA flow process promptly has the absorption of pressure, normal pressure desorb flow process.General adsorptive pressure is 0.2～0.6MPa, adsorption bed desorb under the standard atmosphere pressure condition.This flow process is mainly used in the less separation of air oxygenerator of scale, and characteristics are that equipment is simple, but product recovery rate is low, energy consumption is higher.(2) VSA flow process, i.e. normal pressure absorption, vacuum desorption flow process.Adsorptive pressure is a normal pressure or a little more than barometric point, utilizes vacuum pump to vacuumize desorb.Be mainly used in larger gas separation unit, characteristics are product recovery rate height, and energy consumption is lower, but the equipment relative complex, the initial cost height.The barometric point of high altitude localities (refering in particular to height above sea level here above the area more than 4000 meters) is well below standard atmosphere pressure.Owing to be subjected to the influence of environmental stress, adopt the transformation fractionation by adsorption air oxygenerator of PSA flow process and VSA flow process often can not normally move or efficiently operation in the high altitude localities.But along with extensively carrying out of development of the West Regions and construction, grow with each passing day to the demand of oxygen in the high altitude localities.Therefore, be necessary to develop a kind of pressure swing adsorption oxygen making device that is applicable to the high altitude localities.
Summary of the invention
The object of the invention is to provide that a kind of equipment is simple, product recovery rate is high, energy consumption is lower, is applicable to the pressure swing adsorption oxygen making device of high altitude localities that being called has the pressure swing adsorption oxygen making device of pressing absorption low pressure desorb (being called for short LPSA) flow process.
A kind ofly be suitable for the pressure swing adsorption oxygen making device that the high altitude localities is used, by oil-free air compressor 1, air-cooler 2, adsorption tower 4, adsorption tower 5, product gas gas-holder 6, operated pneumatic valve 7,8,9,10,12,13,14, reducing valve 15, needle type valve 11, under meter 16, flow control valve 17 parts such as grade constitute, it is characterized in that being provided with in the device unstripped gas gas-holder 3, the effect of unstripped gas gas-holder 3 is a pressure of stablizing the adsorption bed outlet, store the compressor air-discharging in the pressure equalizing, reduce the influence of the fluctuation of product airshed and environmental stress device performance.Surpass area more than 4000 meters for height above sea level, because high altitude localities air rarefaction, system normally moves for assurance, the exhaust pressure of air compressor is 0.1～0.7Mpa, the volume of unstripped gas gas-holder is 1.1～3 times of adsorption tower volumetrical, and required raw material source of the gas capacity coupling is 21～50 times of product tolerance.
Whole prod making processes is: air enters air-cooler 2 coolings, the incoming stock gas gas-holder 3 of cooled gas after oil free compressor 1 compression.Pneumavalve 7,10 and 13 leaves, and valve 8,9,12,14 cuts out.This moment, adsorption tower 4 was in absorption phase, and adsorption tower 5 is in desorption phase.Enter adsorption tower 4 from the high pressure mixed gas of unstripped gas gas-holder 3 through valve 7, the adsorptive pressure in the adsorption tower is 0.2MPa～0.5MPa.In adsorption tower 4, the strong absorbed component-nitrogen in the unstripped gas is adsorbed the zeolite molecular sieve absorption in the tower.Weak absorbed component in the unstripped gas--oxygen is discharged from adsorption tower 4 outlets.Wherein a part enters product gas gas-holder 6 as product gas through pneumavalve 13, reducing valve 15.And another part oxygen reverse adsorption tower 5 that enters after needle type valve 11 step-downs that adsorption tower 4 produces cleans the molecular sieve bed that is in desorption state.The waste gas of the desorb of adsorption tower 5 directly is discharged in the surrounding environment through valve 10.Because the high altitude localities environmental stress is far below standard atmosphere pressure, this moment, adsorption tower 5 was equivalent to desorb under vacuum condition.Molecular sieve bed in adsorption tower 4 is near before saturated, and valve 7,8,9,10,13,14 cuts out, and valve 12 leaves.Adsorption tower 4 is finished absorption phase, and adsorption tower 5 is finished the desorption and regeneration stage.Subsequently, a part of gas in the adsorption tower 4 enters 5, two adsorption towers of adsorption tower through equalizing valve 12 and carries out pressure equalizing.Adsorption tower 4 pressure reduce, and adsorption tower 5 pressure raise, the oxygen components that recovery part mechanical energy and concentration are higher.In the pressure equalizing, two adsorption towers 4 and 5 all stop into unstripped gas.At this moment, the compressor expellant gas stores at unstripped gas gas-holder 3.After all the pressure stage finished, valve 8,9,14 left, and valve 7,10,12,13 cuts out, adsorption tower 4 decompression desorbs, adsorption tower 5 absorption of boosting.Before adsorption bed 5 reaches capacity, stop air inlet.Thereby finish a transformation sorption cycle cycle.Two adsorption towers are alternately finished absorption and desorption process just can produce oxygen continuously from the product end.Pressure in the absorption phase, adsorption tower is 0.2MPa～0.5MPa.Directly desorb under local barometric point (absolute pressure is less than 0.1MPa) condition did not adopt vacuum pump to vacuumize after adsorption tower reached capacity.When sea level elevation was 5000m, the desorption pressures of adsorption tower was (absolute pressure) about 0.05MPa.The product gas that obtains from the adsorption bed outlet enters product gas gas-holder 6 after reducing valve 15 decompressions.According to the actual needs, the oxygen concentration of product gas can be regulated between 80%-95%.
The present invention had both solved the problem that the source of the gas deficiency that the high altitude localities environment atmospheric pressure is low, air rarefaction caused and adsorptive pressure do not reach design load, made full use of the characteristics that subatmospheric helps the pressure-swing adsorption process desorb again, reached with vacuum pump and to vacuumize obtained effect.This pressure swing adsorption oxygen making device can be breathed and health care usefulness oxygen and relevant industrial oxygen for the construction of high altitude localities and staff provide, and has that equipment is simple, easy to adjust, the level of automation advantages of higher.
Description of drawings
Fig. 1 is a LPSA flow process making oxygen synoptic diagram.
Wherein: 1-compressor, 2-air-cooler, 3-unstripped gas gas-holder, 4, the 5-adsorption tower, 6-product gas gas-holder, 7,8,9,10,13, the 14-operated pneumatic valve, 12-equalizing valve, 15-reducing valve, 11-needle type valve, 16-under meter, 17-flow control valve
Embodiment
Embodiment 1, and air enters air-cooler 2 coolings after oil free compressor 1 compression.The incoming stock gas gas-holder 3 of cooled gas, the volume of unstripped gas gas-holder 3 are 1.2 times of adsorption tower volumetrical, and required raw material source of the gas capacity coupling is 25 times of product tolerance.Open pneumavalve 7,10 and 13, valve 8,9,12,14 cuts out, and this moment, adsorption tower 4 was in absorption phase, and adsorption tower 5 is in desorption phase.Enter adsorption tower 4 from the high pressure mixed gas of unstripped gas gas-holder 3 through valve 7, the adsorptive pressure in the adsorption tower is 0.2MPa.In adsorption tower 4, the strong absorbed component-nitrogen in the unstripped gas is adsorbed the zeolite molecular sieve absorption in the bed.Weak absorbed component-oxygen in the unstripped gas is discharged from the adsorption tower outlet.Wherein a part enters product gas gas-holder 6 as product gas through pneumavalve 13, reducing valve 15.And another part oxygen reverse adsorption tower 5 that enters after needle type valve 11 step-downs that adsorption tower 4 produces cleans the molecular sieve bed that is in desorption state.The waste gas of the desorb of adsorption tower 5 directly is discharged in the surrounding environment through valve 10.Molecular sieve bed in adsorption tower 4 is near before saturated, and valve 7,8,9,10,13,14 cuts out, and valve 12 leaves.Adsorption tower 4 is finished absorption phase, and adsorption tower 5 is finished the desorption and regeneration stage.Subsequently, a part of gas in the adsorption tower 4 enters 5, two adsorption towers of adsorption tower through equalizing valve 12 and carries out pressure equalizing.Adsorption tower 4 pressure reduce, and adsorption tower 5 pressure raise, the oxygen components that recovery part mechanical energy and concentration are higher.In the pressure equalizing, two adsorption towers 4 and 5 all stop into unstripped gas.At this moment, the compressor expellant gas stores at unstripped gas gas-holder 3.After all the pressure stage finished, valve 8,9,14 left, and valve 7,10,12,13 cuts out, adsorption tower 4 decompression desorbs, adsorption tower 5 absorption of boosting.Before adsorption bed 5 reaches capacity, stop air inlet.Thereby finish a transformation sorption cycle cycle.Two adsorption towers are alternately finished absorption and desorption process just can produce oxygen continuously from the product end.The product gas that obtains from the adsorption tower outlet enters product gas gas-holder 6 after the reducing valve decompression.According to actual needs, the oxygen concentration of product gas can be regulated between 80%-95%.
Embodiment 2, and air enters air-cooler 2 coolings after oil free compressor 1 compression.The incoming stock gas gas-holder 3 of cooled gas.The volume of unstripped gas gas-holder 3 is 1.5 times of adsorption tower volumetrical, and required raw material source of the gas capacity coupling is 30 times of product tolerance.Open pneumavalve 7,10 and 13, valve 8,9,12,14 cuts out.This moment, adsorption tower 4 was in absorption phase, and adsorption tower 5 is in desorption phase.Enter adsorption tower 4 from the high pressure mixed gas of unstripped gas gas-holder 3 through valve 7, the adsorptive pressure in the adsorption tower is 0.3MPa.In adsorption tower 4, the strong absorbed component-nitrogen in the unstripped gas is adsorbed the zeolite molecular sieve absorption in the tower.Weak absorbed component-oxygen in the unstripped gas is discharged from the adsorption tower outlet.Wherein a part enters product gas gas-holder 6 as product gas through pneumavalve 13, reducing valve 15.And another part oxygen reverse adsorption bed 5 that enters after needle type valve 11 step-downs that adsorption tower 4 produces cleans the molecular sieve bed that is in desorption state.The waste gas of the desorb of adsorption tower 5 directly is discharged in the surrounding environment through valve 10.Molecular sieve bed in adsorption tower 4 is near before saturated, and valve 7,8,9,10,13,14 cuts out, and valve 12 leaves.Adsorption tower 4 is finished absorption phase, and adsorption tower 5 is finished the desorption and regeneration stage.Subsequently, a part of gas in the adsorption tower 4 enters 5, two adsorption towers of adsorption tower through equalizing valve 12 and carries out pressure equalizing.Adsorption tower 4 pressure reduce, and adsorption tower 5 pressure raise, the oxygen components that recovery part mechanical energy and concentration are higher.In the pressure equalizing, two adsorption towers 4 and 5 all stop into unstripped gas.At this moment, the compressor expellant gas stores at unstripped gas gas-holder 3.After all the pressure stage finished, valve 8,9,14 left, and valve 7,10,12,13 cuts out, adsorption tower 4 decompression desorbs, adsorption tower 5 absorption of boosting.Before adsorption bed 5 reaches capacity, stop air inlet.Thereby finish a transformation sorption cycle cycle.Two adsorption towers are alternately finished absorption and desorption process just can produce oxygen continuously from the product end.The product gas that obtains from the adsorption tower outlet enters product gas gas-holder 6 after the reducing valve decompression.
Embodiment 3, and air enters air-cooler 2 coolings after oil free compressor 1 compression.The incoming stock gas gas-holder 3 of cooled gas.The volume of unstripped gas gas-holder 3 is 2 times of adsorption tower volumetrical, and required raw material source of the gas capacity coupling is 40 times of product tolerance.Open pneumavalve 7,10 and 13, valve 8,9,12,14 cuts out.This moment, adsorption tower 4 was in absorption phase, and adsorption tower 5 is in desorption phase.Enter adsorption tower 4 from the high pressure mixed gas of unstripped gas gas-holder 3 through valve 7, the adsorptive pressure in the adsorption tower is 0.5MPa.In adsorption tower 4, the strong absorbed component-nitrogen in the unstripped gas is adsorbed the zeolite molecular sieve absorption in the bed.Weak absorbed component-oxygen in the unstripped gas is discharged from the adsorption tower outlet.Wherein a part enters product gas gas-holder 6 as product gas through pneumavalve 13, reducing valve 15.And another part oxygen reverse adsorption tower 5 that enters after needle type valve 11 step-downs that adsorption tower 4 produces cleans the molecular sieve bed that is in desorption state.The waste gas of the desorb of adsorption tower 5 directly is discharged in the surrounding environment through valve 10.Molecular sieve bed in adsorption tower 4 is near before saturated, and valve 7,8,9,10,13,14 cuts out, and valve 12 leaves.Adsorption tower 4 is finished absorption phase, and adsorption tower 5 is finished the desorption and regeneration stage.Subsequently, a part of gas in the adsorption tower 4 enters 5, two adsorption towers of adsorption tower through equalizing valve 12 and carries out pressure equalizing.Adsorption tower 4 pressure reduce, and adsorption tower 5 pressure raise, the oxygen components that recovery part mechanical energy and concentration are higher.In the pressure equalizing, two adsorption towers 4 and 5 all stop into unstripped gas.At this moment, the compressor expellant gas stores at unstripped gas gas-holder 3.After all the pressure stage finished, valve 8,9,14 left, and valve 7,10,12,13 cuts out, adsorption tower 4 decompression desorbs, adsorption tower 5 absorption of boosting.Before adsorption bed 5 reaches capacity, stop air inlet.Thereby finish a transformation sorption cycle cycle.Two adsorption towers are alternately finished absorption and desorption process just can produce oxygen continuously from the product end.The product gas that obtains from the adsorption tower outlet enters product gas gas-holder 6 after the reducing valve decompression.
Embodiment 4, and air enters air-cooler 2 coolings after oil free compressor 1 compression.The incoming stock gas gas-holder 3 of cooled gas.The volume of unstripped gas gas-holder 3 is 3 times of adsorption tower volumetrical, and required raw material source of the gas capacity coupling is 50 times of product tolerance.Open pneumavalve 7,10 and 13, valve 8,9,12,14 cuts out.This moment, adsorption tower 4 was in absorption phase, and adsorption tower 5 is in desorption phase.Enter adsorption tower 4 from the high pressure mixed gas of unstripped gas gas-holder 3 through valve 7, the adsorptive pressure in the adsorption tower is 0.5MPa.In adsorption tower 4, the strong absorbed component-nitrogen in the unstripped gas is adsorbed the zeolite molecular sieve absorption in the bed.Weak absorbed component-oxygen in the unstripped gas is discharged from the adsorption tower outlet.Wherein a part enters product gas gas-holder 6 as product gas through pneumavalve 13, reducing valve 15.And another part oxygen reverse adsorption tower 5 that enters after needle type valve 11 step-downs that adsorption tower 4 produces cleans the molecular sieve bed that is in desorption state.The waste gas of the desorb of adsorption tower 5 directly is discharged in the surrounding environment through valve 10.Molecular sieve bed in adsorption tower 4 is near before saturated, and valve 7,8,9,10,13,14 cuts out, and valve 12 leaves.Adsorption tower 4 is finished absorption phase, and adsorption tower 5 is finished the desorption and regeneration stage.Subsequently, a part of gas in the adsorption tower 4 enters 5, two adsorption towers of adsorption tower through equalizing valve 12 and carries out pressure equalizing.Adsorption tower 4 pressure reduce, and adsorption tower 5 pressure raise, the oxygen components that recovery part mechanical energy and concentration are higher.In the pressure equalizing, two adsorption towers 4 and 5 all stop into unstripped gas.At this moment, the compressor expellant gas stores at unstripped gas gas-holder 3.After all the pressure stage finished, valve 8,9,14 left, and valve 7,10,12,13 cuts out, adsorption tower 4 decompression desorbs, adsorption tower 5 absorption of boosting.Before adsorption bed 5 reaches capacity, stop air inlet.Thereby finish a transformation sorption cycle cycle.Two adsorption towers are alternately finished absorption and desorption process just can produce oxygen continuously from the product end.The product gas that obtains from the adsorption tower outlet enters product gas gas-holder 6 after the reducing valve decompression.
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| CN 200310122470 CN1228128C (en) | 2003-12-25 | 2003-12-25 | Variable pressure adsorptive oxygen making device suitable for high altitude area |
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| CN 200310122470 CN1228128C (en) | 2003-12-25 | 2003-12-25 | Variable pressure adsorptive oxygen making device suitable for high altitude area |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20140345609A1 (en) * | 2011-09-13 | 2014-11-27 | Douglas Adam Whitcher | Portable oxygen concentrator |
| CN110750753B (en) * | 2019-10-21 | 2023-08-22 | 中国人民解放军陆军军医大学 | Method for estimating oxygen demand of large-scale crowd entering high-altitude area |
| CN110980651A (en) * | 2019-12-27 | 2020-04-10 | 广西珂深威医疗科技有限公司 | Oxygen generation system based on bidirectional complementary oxygen pressure equalization |
| CN111847388B (en) * | 2020-06-19 | 2025-05-09 | 华中科技大学同济医学院附属同济医院 | A pressure swing adsorption oxygen generator |
| CN111659228B (en) * | 2020-06-30 | 2022-05-06 | 佛山市美客医疗科技有限公司 | Working method of pressure swing adsorption oxygen equipment |
| CN112516749B (en) * | 2020-06-30 | 2022-07-05 | 上海海尔医疗科技有限公司 | Pressure swing adsorption oxygen equipment |
| CN114949647A (en) * | 2022-06-06 | 2022-08-30 | 北京航空航天大学 | System and method for preparing breathing gas by extracting oxygen |
| CN115228240B (en) * | 2022-07-20 | 2023-04-18 | 广西珂深威医疗科技有限公司 | Oxygen generation system and oxygen generation method suitable for low-oxygen-concentration purification in multiple scenes |
| CN115591364A (en) * | 2022-10-25 | 2023-01-13 | 北京复风纯化科技有限公司（Cn） | A high-purity gas preparation method and system |
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