USRE43398E1 - Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator - Google Patents
Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator Download PDFInfo
- Publication number
- USRE43398E1 USRE43398E1 US11/366,986 US36698606A USRE43398E US RE43398 E1 USRE43398 E1 US RE43398E1 US 36698606 A US36698606 A US 36698606A US RE43398 E USRE43398 E US RE43398E
- Authority
- US
- United States
- Prior art keywords
- oxygen
- dewar
- liquid
- swing adsorption
- pressure swing
- 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 - Lifetime
Links
- 239000001301 oxygen Substances 0.000 title claims abstract description 312
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 312
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract 154
- 239000007788 liquid Substances 0.000 title claims description 116
- 238000000034 method Methods 0.000 title claims description 49
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 286
- 238000003860 storage Methods 0.000 claims abstract description 92
- 239000007789 gas Substances 0.000 claims abstract description 81
- 238000004891 communication Methods 0.000 claims abstract description 19
- 239000012080 ambient air Substances 0.000 claims abstract description 12
- 229910001882 dioxygen Inorganic materials 0.000 claims abstract description 10
- 239000012530 fluid Substances 0.000 claims abstract description 9
- 238000001179 sorption measurement Methods 0.000 claims description 53
- 238000012546 transfer Methods 0.000 claims description 26
- 238000009833 condensation Methods 0.000 claims description 20
- 230000005494 condensation Effects 0.000 claims description 20
- 230000001965 increasing effect Effects 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 17
- 230000007246 mechanism Effects 0.000 claims description 17
- 239000002808 molecular sieve Substances 0.000 claims description 15
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 15
- 239000003570 air Substances 0.000 claims description 13
- 230000005484 gravity Effects 0.000 claims description 13
- 239000012535 impurity Substances 0.000 claims description 13
- 238000013022 venting Methods 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- 238000012544 monitoring process Methods 0.000 claims description 7
- 239000006200 vaporizer Substances 0.000 claims description 7
- 238000010926 purge Methods 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 239000000356 contaminant Substances 0.000 claims description 4
- 230000002708 enhancing effect Effects 0.000 claims description 4
- 238000007710 freezing Methods 0.000 claims description 2
- 230000008014 freezing Effects 0.000 claims description 2
- 230000008878 coupling Effects 0.000 claims 4
- 238000010168 coupling process Methods 0.000 claims 4
- 238000005859 coupling reaction Methods 0.000 claims 4
- 239000000411 inducer Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 42
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 26
- 239000000203 mixture Substances 0.000 description 23
- 229910052757 nitrogen Inorganic materials 0.000 description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- 229910052786 argon Inorganic materials 0.000 description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- 230000000153 supplemental effect Effects 0.000 description 9
- 238000009835 boiling Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- 239000003507 refrigerant Substances 0.000 description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 6
- 229910052802 copper Inorganic materials 0.000 description 6
- 239000010949 copper Substances 0.000 description 6
- 238000009825 accumulation Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 238000002640 oxygen therapy Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000006870 function Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 208000006545 Chronic Obstructive Pulmonary Disease Diseases 0.000 description 2
- 206010021143 Hypoxia Diseases 0.000 description 2
- 208000019693 Lung disease Diseases 0.000 description 2
- VVTSZOCINPYFDP-UHFFFAOYSA-N [O].[Ar] Chemical compound [O].[Ar] VVTSZOCINPYFDP-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 230000000007 visual effect Effects 0.000 description 2
- 208000030507 AIDS Diseases 0.000 description 1
- 206010014561 Emphysema Diseases 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- OLBVUFHMDRJKTK-UHFFFAOYSA-N [N].[O] Chemical compound [N].[O] OLBVUFHMDRJKTK-UHFFFAOYSA-N 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 208000006673 asthma Diseases 0.000 description 1
- 235000013405 beer Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000008280 blood Substances 0.000 description 1
- 210000004369 blood Anatomy 0.000 description 1
- 210000004556 brain Anatomy 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000003467 diminishing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 210000002216 heart Anatomy 0.000 description 1
- 208000019622 heart disease Diseases 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical group [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 208000018875 hypoxemia Diseases 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 210000003734 kidney Anatomy 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- 208000014055 occupational lung disease Diseases 0.000 description 1
- 210000000056 organ Anatomy 0.000 description 1
- 238000009428 plumbing Methods 0.000 description 1
- 208000005069 pulmonary fibrosis Diseases 0.000 description 1
- 201000003651 pulmonary sarcoidosis Diseases 0.000 description 1
- 230000000241 respiratory effect Effects 0.000 description 1
- 210000002345 respiratory system Anatomy 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 230000005236 sound signal Effects 0.000 description 1
- 238000002560 therapeutic procedure Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 230000003442 weekly effect Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0454—Controlling adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C6/00—Methods and apparatus for filling vessels not under pressure with liquefied or solidified gases
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0017—Oxygen
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0276—Laboratory or other miniature devices
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M2202/00—Special media to be introduced, removed or treated
- A61M2202/02—Gases
- A61M2202/0208—Oxygen
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M2202/00—Special media to be introduced, removed or treated
- A61M2202/03—Gases in liquid phase, e.g. cryogenic liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/116—Molecular sieves other than zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/502—Carbon monoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40007—Controlling pressure or temperature swing adsorption
- B01D2259/40009—Controlling pressure or temperature swing adsorption using sensors or gas analysers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/4525—Gas separation or purification devices adapted for specific applications for storage and dispensing systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/4533—Gas separation or purification devices adapted for specific applications for medical purposes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/4541—Gas separation or purification devices adapted for specific applications for portable use, e.g. gas masks
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/455—Gas separation or purification devices adapted for specific applications for transportable use
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/053—Pressure swing adsorption with storage or buffer vessel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2201/00—Vessel construction, in particular geometry, arrangement or size
- F17C2201/05—Size
- F17C2201/058—Size portable (<30 l)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2203/00—Vessel construction, in particular walls or details thereof
- F17C2203/03—Thermal insulations
- F17C2203/0391—Thermal insulations by vacuum
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
- F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
- F17C2205/0302—Fittings, valves, filters, or components in connection with the gas storage device
- F17C2205/0323—Valves
- F17C2205/0326—Valves electrically actuated
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
- F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
- F17C2205/0302—Fittings, valves, filters, or components in connection with the gas storage device
- F17C2205/0323—Valves
- F17C2205/0332—Safety valves or pressure relief valves
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
- F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
- F17C2205/0302—Fittings, valves, filters, or components in connection with the gas storage device
- F17C2205/0341—Filters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2221/00—Handled fluid, in particular type of fluid
- F17C2221/01—Pure fluids
- F17C2221/011—Oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
- F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
- F17C2223/0146—Two-phase
- F17C2223/0153—Liquefied gas, e.g. LPG, GPL
- F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/03—Heat exchange with the fluid
- F17C2227/0337—Heat exchange with the fluid by cooling
- F17C2227/0341—Heat exchange with the fluid by cooling using another fluid
- F17C2227/0353—Heat exchange with the fluid by cooling using another fluid using cryocooler
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/04—Methods for emptying or filling
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/03—Control means
- F17C2250/032—Control means using computers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/04—Indicating or measuring of parameters as input values
- F17C2250/0404—Parameters indicated or measured
- F17C2250/0408—Level of content in the vessel
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/04—Indicating or measuring of parameters as input values
- F17C2250/0404—Parameters indicated or measured
- F17C2250/043—Pressure
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/04—Indicating or measuring of parameters as input values
- F17C2250/0404—Parameters indicated or measured
- F17C2250/0439—Temperature
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/04—Indicating or measuring of parameters as input values
- F17C2250/0404—Parameters indicated or measured
- F17C2250/0447—Composition; Humidity
- F17C2250/0452—Concentration of a product
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2260/00—Purposes of gas storage and gas handling
- F17C2260/02—Improving properties related to fluid or fluid transfer
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/01—Purifying the fluid
- F17C2265/015—Purifying the fluid by separating
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2270/00—Applications
- F17C2270/02—Applications for medical applications
- F17C2270/025—Breathing
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2270/00—Applications
- F17C2270/05—Applications for industrial use
- F17C2270/0509—"Dewar" vessels
-
- 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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
- F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
-
- 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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/14—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the cycle used, e.g. Stirling cycle
- F25B9/145—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the cycle used, e.g. Stirling cycle pulse-tube cycle
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
- F25J2270/91—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration using pulse tube refrigeration
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Definitions
- the field of this invention relates to using an oxygen concentrator to create a portable supply of supplementary oxygen for ambulatory respiratory patients so that they can lead normal and productive lives—as the typical primary oxygen sources are too bulky to carry or require excessive power to operate.
- Supplemental oxygen is necessary for patients suffering from lung disorders; for example, pulmonary fibrosis, sarcoidosis, or occupational lung disease.
- oxygen therapy is an increasingly beneficial, life-giving development.
- supplemental oxygen increases blood oxygenation, which reverses hypoxemia.
- This therapy prevents long-term effects of oxygen deficiency on organ systems—in particular, the heart, brain and kidneys.
- Oxygen treatment is also prescribed for Chronic Obstructive Pulmonary Disease (COPD), which afflicts about 25 million people in the U.S., and for other ailments that weaken the respiratory system, such as heart disease and AIDS.
- COPD Chronic Obstructive Pulmonary Disease
- Supplemental oxygen therapy is also prescribed for asthma and emphysema.
- the normal prescription for COPD patients requires supplemental oxygen flow via nasal cannula or mask twenty four hours per day.
- the average patient prescription is two liters per minute of high concentration oxygen to increase the oxygen level of the total air inspired by the patient from the normal 21% to about 40%. While the average oxygen flow requirement is two liters per minute, the average oxygen concentrator has a capacity of four to six liters of oxygen per minute. This extra capacity is occasionally necessary for certain patients who have developed more severe problems but they are not generally able to leave the home (as ambulatory patients) and do not require a portable oxygen supply.
- Either modality may be used for both in-home and ambulatory use or may be combined with an oxygen concentrator which would provide in-home use.
- the major drawback of the gaseous oxygen option is that the small cylinders of gaseous oxygen can only provide gas for a short duration.
- Oxygen conserving devices that limit the flow of oxygen to the time of inhalation may be used.
- the conserving devices add to the cost of the service and providers have been reluctant to add it because there often is no health insurance reimbursement. Indeed, the insurance reimbursement for medical oxygen treatment appears to be shrinking.
- liquid oxygen storage option its main drawback is that it requires a base reservoir—a stationary reservoir base unit about the size of a standard beer keg—which has to be refilled about once a week.
- the liquid oxygen can then be obtained from a base unit and transferred to portable dewars which can be used by ambulatory patients.
- there is substantial waste as a certain amount of oxygen is lost during the transfer to the portable containers and from evaporation. It is estimated that 20% of the entire contents of the base cylinder will be lost in the course of two weeks because of losses in transfer and normal evaporation. These units will typically boil dry over a period of 30 to 60 days even if no oxygen is withdrawn.
- supplemental oxygen is supplied to the patient by a home care provider, in exchange for which it receives a fixed monetary payment from insurance companies or Medicare regardless of the modality.
- Oxygen concentrators for use in the home are preferred and are the least expensive option for the home care provider.
- Oxygen concentrators for use in the home are preferred and are the least expensive option for the home care provider.
- One of these two modalities may be used for both in-home and ambulatory use or may be combined with an oxygen concentrator which would provide in-home use. In either case, the home care provider must make costly weekly or biweekly trips to the patient's home to replenish the oxygen.
- One of the objects of this invention is to eliminate these costly “milk runs.”
- An aspect of the present invention involves a home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator is condensed into liquid oxygen.
- the system includes an oxygen concentrator which separates oxygen gas from the ambient air, a condenser in communication with the oxygen concentrator for receiving and liquefying the oxygen gas flow, a cryocooler associated with the condenser, and a first storage dewar in fluid communication with the condenser and adapted to store the oxygen liquefied by the condenser, the first storage dewar including means for transferring liquid oxygen from the first dewar to a second dewar for storing a quantity of oxygen suitable for moveable oxygen treatment.
- the liquid oxygen transferring means is adapted to increase the pressure in the first dewar.
- the liquid transferring means includes a heater immersed within the liquid oxygen in the first dewar.
- the first dewar includes an inner vessel in which the liquid oxygen reside, and liquid transferring means includes a heater attached to the outer surface of inner vessel.
- the liquid transferring means includes a high-pressure compressor in communication with the concentrator for delivering high-pressure air thereto.
- the liquid transferring means includes a vaporizer loop associated with the first dewar.
- the liquid transferring means includes a controllable heat leak associated with the first dewar.
- the liquid transferring means includes a gravity-assisted dispensing mechanism.
- system further includes the second storage dewar and the second storage dewar is adapted to be filled at a pressure below 20 psig.
- An additional aspect of the invention involves a home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator is condensed into liquid oxygen.
- the system includes an oxygen concentrator which separates oxygen gas from the ambient air, a condenser in communication with the oxygen concentrator for receiving and liquefying the oxygen gas flow, a cryocooler associated with the condenser, and a portable dewar adapted to interface with the condenser and adapted to store the oxygen liquefied by the condenser.
- the method includes generating a gaseous supply of oxygen using the oxygen concentrator; splitting off at least a portion of the gaseous supply to be liquefied; cooling the supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen; storing the liquid oxygen in the storage dewar; and transferring the liquid oxygen in the storage dewar with the liquid oxygen transferring means to a second dewar for storing a quantity of liquid oxygen from which smaller quantities can be transferred for moveable oxygen treatment.
- transferring the liquid oxygen includes increasing the pressure in the first dewar.
- the liquid transferring means includes a heater immersed within the liquid oxygen in the first dewar and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar.
- the first dewar includes an inner vessel in which the liquid oxygen reside
- the liquid transferring means includes a heater attached to the outer surface of inner vessel
- transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar
- the condenser is in communication with the concentrator through a line
- the liquid transferring means includes a compressor located in the line between the condenser and the concentrator, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering the condenser and the dewar with the compressor.
- the liquid transferring means includes a high-pressure compressor in communication with the concentrator for delivering high-pressure air thereto, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering the condenser and the dewar with the compressor.
- the liquid transferring means includes a vaporizer loop associated with the first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar with the vaporizer loop so that the pressure is increased in the first dewar.
- the liquid transferring means includes a controllable heat leak associated with the first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar.
- system further includes the second storage dewar, the second storage dewar is adapted to filled at a pressure below 20 psig.
- the home liquid oxygen ambulatory system includes an oxygen concentrator for delivering gaseous flow to the liquefier and a storage dewar having an inner vessel for storing liquid oxygen produced by the liquefier.
- the liquefier includes a condenser, a refrigerating device associated with the condenser, means for communicating incoming gaseous flow from the oxygen concentrator to the condenser, the communicating means having an inner surface with a dimension D, means for venting gaseous flow not condensed from the inner vessel, the venting means having an outer surface with an dimension d, and whereby the dimension D of the inner surface of the communicating means is significantly larger than the dimension d of the outer surface of the venting means to allow for the build-up of solid contaminants on the outer surface of the venting means without plugging up the communicating means.
- the venting means includes a recuperator comprised of a helical coil of tubing, the tubing having the outer surface with a diameter of the dimension d, whereby the incoming gas stream flows over the outer surface of the helical coil of tubing and a vent stream flows inside the helical coil of tubing.
- the outer surface of the helical coil of tubing has a cold surface to freeze out trace impurities of solid contaminants such as H2O, CO2 and hydrocarbons.
- the communicating means is comprised of a neck tube having the inner surface with a diameter of the dimension D.
- the liquefier further includes a liquid withdrawal tube located central to the refrigerating device, recuperator and condenser for removing liquid oxygen from the storage dewar.
- the refrigerating device is integral with the condenser.
- the refrigerating device, condenser and recuperator are integral with the storage dewar.
- Another aspect of the invention involves a method for generating liquid oxygen in a home from a home liquid oxygen ambulatory system having an oxygen concentrator, a condenser, a cryocooler, a recuperator and a storage dewar.
- the method includes generating a gaseous supply of oxygen, which includes some trace impurities, using the oxygen concentrator; splitting off at least a portion of the gaseous supply to be liquefied; cooling the supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen; condensing less than all of the gaseous oxygen supply flowing into the condenser; freezing out the trace impurities of the gaseous supply of oxygen and venting the non-condensed nitrogen, argon and oxygen with the recuperator; storing the liquid oxygen in the storage dewar; and periodically removing accumulated frozen impurities on the recuperator by boiling-off any stored liquid oxygen and then flow purging the system until the system has reached room temperature.
- the condenser includes a generally vertically oriented tubular member adapted to conduct heat axially to the refrigerating device, the tubular member having outer and inner surfaces, at least one of the outer and inner surfaces having a plurality of generally vertically oriented flutes and convex fins adapted to increase the condensation rate per unit area by thinning the liquid film and drain the condensate to keep the condensate from flooding the condensation surfaces.
- the fins have a hyperbolic cosine profile.
- the flutes have a profile selected from the group consisting of concave, generally V-shaped, generally rectilinear.
- the plurality of generally vertically oriented flutes and convex fins are located on both the outer and inner surfaces.
- the condenser includes a generally vertically oriented tubular member adapted to conduct heat axially to the refrigerating device, the tubular member having outer and inner surfaces, at least one of the outer and inner surfaces includes means for enhancing the condensation rate per unit area by maintaining a small liquid film thickness on the condensation surfaces.
- the condensation enhancing means includes a plurality of generally vertically oriented flutes and convex fins.
- the fins have a hyperbolic cosine profile.
- the flutes have a profile selected from the group consisting of concave, generally V-shaped, generally rectilinear.
- the plurality of generally vertically oriented flutes and convex fins are located on both the outer and inner surfaces.
- FIG. 1 is a block diagram of the invention in the medical oxygen preferred embodiment where gaseous oxygen is split off and liquefied for storage in a stationary dewar or container.
- FIG. 2 shows another preferred embodiment of the invention for ambulatory supplemental oxygen using a portable LOX dewar.
- FIG. 3 shows a typical temperature-composition diagram for oxygen-argon mixtures at typical dewar pressures.
- FIG. 4 shows a typical temperature-composition diagram for nitrogen-oxygen mixtures at typical dewar pressures.
- FIG. 5 shows typical oxygen concentration test data for gas streams into the condenser and out of the dewar during liquefaction, and out of the dewar as the liquid is re-vaporized.
- Oxygen source is a PSA oxygen concentrator.
- FIG. 6 shows the controller block diagram for operation of the system.
- FIGS. 7A through 7D are flow charts showing the controller logic.
- FIG. 8 shows the controller input levels and output states for the start-up mode of the preferred embodiment.
- FIG. 9 shows the controller input levels and output states for the condense mode of the preferred embodiment.
- FIG. 11 shows the controller input levels and output state for the boil dry mode of the preferred embodiment.
- FIG. 13 illustrates another embodiment of a cryocooler which may be used in the subject invention.
- FIG. 15 is an end cross-sectional view of the preferred embodiment of the condenser corresponding to FIG. 14 .
- FIG. 16 shows a side cross-sectional view of another preferred embodiment of the condenser.
- FIG. 21 is an end cross-sectional view, similar to FIG. 17 , of an embodiment of a condenser having shaped fins to reduce the liquid film thickness.
- FIG. 1 A flow chart of the preferred embodiment of the invention is set out in FIG. 1 .
- Its main components include an oxygen concentrator 11 , a cryocooler 12 , a condenser 13 , and a storage/collection dewar or vacuum insulated container 14 .
- the oxygen concentrator 11 operates on a pressure swing adsorption cycle and essentially strips all or most of the nitrogen from air along with other minor components such as H 2 O, CO 2 , CO, NO x , etc. The result is a stream of dry gas with high oxygen concentration ( ⁇ 92%) flowing in fluid outlet 50 .
- a portion of the gas from this output in fluid outlet 50 is routed to a condenser 13 in association with a cryocooler (or cryogenic refrigerator) 12 through flow lines 51 and 57 .
- the cryocooler provides cooling of the condenser heat exchanger 13 to liquefaction temperatures, causing the oxygen in contact therewith to go from the gaseous to the liquid phase.
- the condenser 13 typically must be insulated from ambient heating and may in practice even be located inside the dewar 14 .
- a recuperator 15 may be used to pre-cool the incoming stream utilizing the vent flow through line 52 out of the dewar as a cooling medium. In practice, this recuperator 15 may also be located within the dewar 14 to reduce ambient heating.
- the dewar 14 could be eliminated and replaced with a portable dewar 23 which is modified slightly from those existing today.
- the new portable dewar would interface with the condenser 13 , recuperator 15 , and controller 16 .
- This embodiment requires a slightly different control scheme from that given for the preferred embodiment as the transfer and boil-dry modes are eliminated. Any small amount of accumulated water and hydrocarbons are eliminated from the portable dewar 23 after each use by allowing it to warm to room temperature before reuse.
- FIG. 1 In operation, in the preferred embodiment of FIG. 1 , where a pressure swing adsorption (“PSA”) system is used, air is drawn into the oxygen concentrator 11 , where it is compressed by an oilless compressor, cooled, and passed through molecular sieve beds operating on the pressure swing adsorption cycle, as shown in U.S. Pat. Nos. 5,366,541; 5,112,367; 5,268,021 and Re. 35,009, which are incorporated herein by reference.
- This PSA system produces a 5-6 liters per minute (LPM) gas stream with high oxygen concentration at 3-7 pounds per square inch gauge (psig).
- LPM pounds per square inch gauge
- the composition of this gas stream varies but is typically 90-95% oxygen, 5-6% argon, 0-4% nitrogen, ⁇ 15 parts per million (ppm) water vapor, and ⁇ 1 ppm hydrocarbons. Exhaust from the PSA cycle (80-84% nitrogen, 15-19% oxygen, 0.6-0.8% argon, and trace amounts of water vapor, carbon dioxide and hydrocarbons) is vented into the atmosphere as waste gas.
- the high concentration oxygen stream in fluid outlet 50 is split with 0-4 lpm going through control valve 24 , for patient consumption, and 0.5-1.5 lpm through line 51 and control valve 19 for liquefaction.
- Oxygen sensor 18 monitors the oxygen concentration produced by oxygen concentrator 11 . If the oxygen concentration falls below 88%, controller 16 will close valve 19 and turn off the cryocooler 12 .
- the initial revaporized stream may have a reduced oxygen content because of the close boiling points of the components of the mixture.
- the temperature of the split gas stream entering the recuperator 15 is about room temperature. It is cooled to about 270 K (or colder) by the vent gas from the dewar flowing through the other side of the recuperator via line 52 .
- the recuperator 15 reduces the load on the cryocooler by using the cold vent gas to pre-cool the oxygen-rich gas stream flowing into the condenser 13 . From the recuperator 15 the high oxygen concentration stream flows through a line 57 to the condenser 13 , which is cooled to ⁇ 90 K by the cryocooler 12 .
- the condenser 13 provides cold surfaces to further cool and condense the flow. It is important to note that the gas passing through the condenser 13 is a mixture of oxygen, argon, and nitrogen. The normal boiling points of these components are: 90.18 K, 87.28 K, and 77.36 K respectively. Because of the close boiling points of the components of this mixture, there was initial skepticism because of the concern that all the nitrogen and argon would condense along with the oxygen.
- FIGS. 3 and 4 are temperature composition diagrams for binary mixtures of oxygen-argon and oxygen-nitrogen.
- FIGS. 3 and 4 are temperature composition diagrams for binary mixtures of oxygen-argon and oxygen-nitrogen.
- the upper curve at a given pressure defines the dew point and the lower curve defines the bubble point.
- FIG. 4 for a pressure of 0.101 MPa, if there is a gas mixture with 10 mole percent nitrogen (point 1 ), condensation will start when the gas has cooled to the dew point curve (point 2 g) which is at a temperature of about 89.5 K in this case.
- the initial liquid formed (point 2 f) will have only 7.4 mole percent nitrogen. If the temperature is lowered to point 3 , the liquid will have the composition of point 3 f while the remaining vapor will have the composition of point 3 g. As the temperature is lowered further to point 4 f or below, all of the mixture liquefies and the composition is 10 mole percent nitrogen, the same as at point 1 . If this liquid is heated, the nitrogen which has a lower boiling point will vaporize first. Thus, the composition of the first vapor formed will be that of point 4 g or about 30 mole percent. As the remaining liquid boils, the mole percent of nitrogen in the vapor drops back to 10 mole percent when point 2 g is reached.
- FIG. 5 shows typical oxygen concentration test data for condensing and re-vaporizing part of the product outlet stream from the oxygen concentrator 11 in the preferred embodiment.
- the system was cooling down without any net liquid accumulation in the dewar 14 . From this point up to about 500 minutes, condensation continued with liquid accumulation.
- the inlet stream to the condenser 13 had an oxygen concentration of 95%, while the vent flow through line 52 had an oxygen concentration of only 92-93%.
- the inlet stream and condenser cooling were stopped.
- the oxygen concentration of the re-vaporized liquid increased as the liquid boiled off due to the lower boiling point components (argon and nitrogen) boiling off first. This change in oxygen concentration presents no problem for medical ambulatory use because the oxygen concentration remains above 85%.
- the amount of incoming flow liquefied is controlled by setting the mass flow rate relative to the cooling capacity of the cryocooler.
- the parameters of the condenser and/or cryocooler can be stored in the memory of the controller and/or computer and the controller regulating the incoming flow depending on the parameters stored and/or sensed. Having a mass flow rate which exceeds the cooling capacity of the cryocooler/condenser combination, prevents the incoming flow from being completely liquefied.
- the mass flow rate is controlled by the amount of flow restriction between inlet valve 19 and flow control valve 25 . This includes the flow losses of the valves themselves as well as those in the recuperator, condenser, and all of the interconnecting plumbing.
- the pressure in the dewar 14 is maintained slightly above ambient pressure while the cryocooler is operating by valve 25 . It is desirable to keep the pressure in the condenser as high as possible because this increases the condensation temperature (as shown in FIGS. 3 and 4 ) which eases the requirements on the cryocooler. Once again this can be controlled by the controller and/or the computer, microprocessor and memory system.
- operating parameters for optimal operation of the system for the condenser should be that the condenser surface temperature should be in the range from 69.2-109.7 K and pressure should be in the range from 5-65 psia.
- the gas concentrations into the condenser for medical use should have oxygen in the range of 80-100%, nitrogen from 0-20%, and argon from 0-7%.
- the pressure in the dewar 14 must be increased so that liquid can be forced up the dip tube 20 .
- heater 21 is used for this purpose. Heater 21 may be immersed in the liquid oxygen or attached to the outer surface of the inner vessel.
- the controller 16 ensures that the cryocooler 12 is turned off and valve 25 is closed before the heater 21 is energized. The heater 21 remains turned on until the pressure, measured by pressure transducer 9 , reaches about 22 psig.
- a further means for transferring liquid by raising the pressure in the dewar 14 includes using a high-pressure compressor 302 within the oxygen concentrator 11 instead of the typical low-pressure compressor.
- the high-pressure compressor 302 has the effect of increasing the pressure in the storage dewar 14 so that when the portable dewar 23 is engaged, liquid is forced up the dip tube 20 .
- a compressor 302 at this location slightly enhances the PSA cycle.
- a still further means for transferring liquid by raising the pressure in the dewar 14 includes using a vaporizer loop 304 .
- the dewar 14 preferably remains at low pressure while liquid is being produced.
- a valve 306 is opened to allow some liquid to flow into a coil 308 to be vaporized. This would increase the pressure in the dewar 14 so that liquid could be transferred to the portable dewar 23 .
- An additional means for transferring liquid without raising the pressure in the dewar 14 includes incorporating a gravity-assisted dispensing mechanism 314 such as a controllable spigot (analogous to those used to dispense liquids from a large insulated cooler) near the bottom of the dewar 14 .
- a gravity-assisted dispensing mechanism 314 such as a controllable spigot (analogous to those used to dispense liquids from a large insulated cooler) near the bottom of the dewar 14 .
- the gravity-assisted dispensing mechanism eliminates the need for the dip tube 20 .
- the gravity-assisted dispensing mechanism 314 preferably includes a quick disconnect valve 316 or other flow control means, similar to disconnect valve 22 described above, located on the end of the mechanism 314 to allow for connection of a portable dewar 23 .
- An additional means for transferring liquid without raising the pressure in the dewar 14 includes incorporating a portable dewar 23 adapted to be filled from a pressure less than 20 psig, which is the standard for currently available home stationary liquid dewars.
- the portable dewar 23 may be adapted to be filled from a pressure such as 5 psig.
- a further means for transferring liquid without raising the pressure in the dewar 14 involves replacing the storage dewar 14 with a specially designed portable dewar 23 such as that described above with respect to FIG. 2 , which interfaces with the rest of the home liquid oxygen ambulatory system.
- the dewar 14 , recuperator 15 , and condenser 13 will be warmed to room temperature periodically (preferably after about 30 fillings of a portable dewar, or every two months). This procedure is accomplished most economically when the inventory of liquid in the storage dewar is low; e.g. shortly after liquid transfer and a portable dewar has been filled.
- valve 19 will be closed, the cryocooler 12 is turned-off, valve 25 is open, and heater 21 is energized until all the liquid has boiled-off as evidenced by, for example, the temperature sensor 10 being above 125 K.
- the neck tube 78 has an inner diameter or dimension D and the helical recuperator 76 is constructed of a tube having an outer diameter or dimension d.
- inner diameter D of the neck tube 78 significantly larger than the outer diameter d of the helical recuperator tube 76 at locations along the neck tube 78 where incoming gaseous flow is present, the liquefier 70 allows for accumulation of frost on the inner surface 84 of the neck tube 78 or outer surface 82 of the recuperator 76 without plugging. This extends the period of time required between boil-dries without causing plugging in the liquefier 70 .
- the cryocooler 97 includes copper tubes 98 , 100 that provide strain relief via respective coils 102 , 104 .
- Copper tube 98 connects the coldhead 96 to a compressor 106 and copper tube 100 connects the coldhead 96 to a reservoir volume 108 .
- a flexible copper braid 110 provides a heat conduction path if needed to reject heat from the coldhead 96 .
- the dewar 14 may include a central liquid withdrawal tube 116 for withdrawing liquid oxygen from the dewar 14 .
- the central liquid withdrawal tube 116 may include an integral liquid level sensor 118 for monitoring the level of the liquid oxygen in the dewar 14 .
- a heater 21 may be attached to the outer surface of the inner vessel of the dewar 14 to assist in transferring liquid oxygen from the dewar 14 .
- the dewar, condenser, recuperator, and all associated hardware are at room temperature and must be cooled down. This is accomplished in the “start-up” mode, where valve 19 (see FIG. 1 ) is open, the heater is off, the cryocooler is on, and valve 25 is modulated to control the pressure/flow rate. It is desired to keep the pressure and hence the density of the gas as high as possible while maintaining the flow rate.
- the higher density gas will have better heat transfer with the dewar walls and associated hardware. It is noted that higher flow rates will enhance the convection heat transfer but may exceed the cooling capacity. Based on the cooling characteristics of the cryocooler between room temperature and 90 K, the flow rate can be changed to minimize the cool-down time.
- the dewar 14 is equipped with at least one relief valve 26 as a safety feature.
- Another relief valve 29 is provided and in communication with the inlet gas stream 51 , before flowing into the recuperator 15 . This serves as a back-up for relief valve 26 as well as providing a means to eliminate accumulated water from the recuperator 15 during periods when the cryocooler 12 is off, if valve 25 is closed.
- a check valve 27 is also provided to prevent backflow into the oxygen concentrator in the event of a malfunction.
- FIG. 6 provides a block diagram of the controller 16 control system with sensor input value ranges and output states. It also shows interfaces to an indicator and a modem or wireless interface.
- the mode switch 28 may be used by the patient to request the system to prepare for a liquid transfer to a portable dewar.
- the indicator then provides a visual signal that the system is building pressure in the dewar. Once the pressure has reached the desired value, a visual and/or audio signal is given to alert the patient that the system is ready to transfer liquid.
- the controller may also be programmed to perform an unattended liquid transfer.
- the modem, telephone line or wireless interface connections are optional hardware that may be added to the controller to enable remote monitoring of the system by the home care provider (e.g., to assist with maintenance and repair) or insurance companies or health providers/administrators (e.g., to assess if patients are using enough ambulatory oxygen to justify payments, etc.).
- the home care provider e.g., to assist with maintenance and repair
- insurance companies or health providers/administrators e.g., to assess if patients are using enough ambulatory oxygen to justify payments, etc.
- FIGS. 7A-D show a logic flow chart for the controller for the normal operation modes. This can also be referred to as the “input/output control schedule.”
- the mode switch 28 can also be used by a repair or factory technician to put the controller in a calibration mode which serves as a method to check and reset the program.
- the indicator provides liquid level readout, transfer request status, and low oxygen concentration information to the patient. All of the sensors are continuously scanned to provide the controller with the latest information.
- FIGS. 8 through 11 provide detailed output states as a function of input levels for the normal operating modes (start-up, condense, transfer, and boil-dry), which can be referred to as the “Optimal Liquefaction Operational Schedule.”
- FIG. 8 relates to the start-up mode; i.e., when the system is first turned on or after the boil-dry cycle.
- the liquid sensor 17 shows zero liquid volume in the dewar and, when the oxygen sensor 18 shows an oxygen concentration greater than 88%, valve 19 is open, heater 21 is off, cryocooler 12 is on, and the indicator or the controller indicates a cool-down state.
- Valve 25 is modulated to control pressure.
- the input to the controller 16 is such that when the oxygen sensor indicates oxygen concentration being greater than 88% and when the other criteria in the left-hand column of FIG. 9 are achieved, the output states set out in the right portion of the chart are attained.
- the liquid level sensor indicates a level of approximately 100%, causing closure of valves 19 and 25 , keeping the heater off, turning the cryocooler off, and having the indicator signal that the dewar is full.
- the transfer mode in FIG. 10 is the stage where one can fill the portable thermos bottles or dewars 23 from the main storage dewar 14 .
- the top portion of FIG. 10 shows controller readouts where, if the liquid sensor indicates a liquid level of less than 20%, then the conclusion is computed that there is not enough liquid to transfer into the portable dewar from the main dewar as shown.
- the heater is activated, and when the pressure sensor indicates that the pressure exceeds 22 psig, as shown on the last line in the left-hand column of FIG. 10 , the heater 21 is then turned off and the controller readout or indicator shows that the transfer of liquid oxygen can be made to the portable dewar.
- FIG. 11 indicates the boil-dry mode, with valve 25 open to allow the vapor to escape, and the various parameters relating thereto.
- FIG. 12 shows a schematic of a pulse tube refrigerator, the preferred embodiment of the cryocooler 12 in FIG. 1 .
- the pulse tube refrigerator is preferred for use in the subject ambulatory oxygen system because of its good efficiency with only one moving part, the pressure oscillator.
- Pulse tube refrigerators are shown in U.S. Pat. Nos. 5,488,830; 5,412,952 and 5,295,355 the disclosure of which are hereby incorporated by reference.
- FIG. 11 depicts a pulse tube refrigerator of the double inlet type.
- Other types of pulse tube refrigerators (PTR) could also be used such as the basic PTR or the inertance tube PTR (Zhu et al., 9 th International Cryocooler Conference, NH, June 1996).
- the double inlet pulse tube refrigerator as shown in FIG. 12 is comprised of a pressure oscillator 30 , primary heat rejecter 31 , regenerator 32 , heat acceptor 33 , pulse tube 34 , orifice rejecter 35 , bypass orifice 36 , primary orifice 37 , and reservoir volume 38 .
- the preferred refrigerant gas in the PTR closed and pressurized circuit is helium but various other gases such as neon or hydrogen could also be used.
- the PTR essentially pumps heat accepted at low temperature in the heat acceptor 33 to the orifice heat rejecter 35 where it is rejected at near ambient temperature.
- FIG. 12 depicts a “U-tube” configuration of the PTR, in-line and coaxial configurations are other possible options. Depicted therein is a piston type pressure oscillator, but other types are possible such as those utilizing diaphragms or bellows.
- FIG. 13 shows a schematic of another embodiment of the cryocooler.
- This is a vapor compression cycle cryocooler using a mixed gas refrigerant such as shown in U.S. Pat. No. 5,579,654; a 1969 German Patent by Fuderer & Andrija; British Patent No. 1,336,892.
- Other types of cryocoolers will work as long as they meet the important criteria of small size, convenience and low cost.
- the refrigerant is compressed by the compressor to high pressure. Then it is cooled by the aftercooler with heat Qh being rejected to the environment. Oil is separated in the oil separator. Oil flows back to the compressor inlet through a flow restriction.
- the refrigerant gas flows to a heat exchanger where it is cooled by the returning cold stream. Some components of the mixture may condense in this process.
- the liquid/gas refrigerant mixture flows through a throttle valve where its pressure is reduced and its temperature drops. This cold refrigerant enters the evaporator where the heat load Qc is absorbed and some liquid is boiled into vapor. This vapor flows up the cold side of the heat exchanger absorbing heat from the incoming stream. Then it flows back to the compressor. Heat Qc is accepted at cold temperature Tc. This is where the condenser would interface with the cryocooler.
- cryocooler it may be possible to remove some of the heat from the oxygen stream at a temperature warmer than Tc.
- FIGS. 14 and 15 One possible geometry of the generally vertically oriented, gravity assisted condenser 13 in FIG. 1 is shown in FIGS. 14 and 15 .
- the incoming gas from the oxygen concentrator flows from conduit 57 to chamber 58 and then is distributed through an annular passage 59 between the outer tube 41 and inner rod 42 .
- the inner rod 42 is made of a high thermal conductivity material such as OFHC (Oxygen Free High Conductivity) copper, to minimize the temperature gradient between the surface on which the oxygen condenses ( 13 ) and the cryocooler 12 .
- the cold end of the cryocooler is shown by cross-hatched member 61 . Due to surface tension, the axial slots or grooves 43 will draw in liquid as it condenses.
- the mass flow rate is chosen to exceed the cooling capacity of the condenser/cryocooler so that only part of the incoming flow is liquefied. Also, the pressure in the condenser is maintained as high as possible while maintaining the desired flow rate. The higher pressure increases the condensation temperature which in turn reduces the requirements on the cryocooler.
- FIGS. 16 and 17 show another embodiment of the condenser that allows easier integration with the mixed gas refrigerant cryocooler. This configuration also allows access to the liquid in the dewar through the center of the condenser.
- the cold end of the cryocooler 45 is in thermal contact with an outer tube 46 and an inner tube 47 , both of which are made of a high thermal conductivity material such as OFHC copper and which utilize flanges 62 and 64 to interface with the cryocooler.
- the inner tube has axial slots or grooves 48 cut into its outer surface (see, FIG. 17 ) to increase the surface area and to wick condensed liquid, preventing a liquid film from forming over its entire surface. Gas enters the condenser through port 63 . The liquid and vapor flow down through an annular passage 49 .
- An isometric view of this embodiment is shown in FIG. 18 .
- FIG. 21 is a cross-sectional view, similar to the views in FIGS. 15 and 17 , of another embodiment of a generally vertically oriented gravity assisted condenser 110 .
- the condenser 110 includes fins 112 and corresponding flutes 114 that extend vertically the longitudinal length of the condenser 110 on both an exterior side 116 and an interior side 118 of the condenser 110 , generally parallel with a vertical longitudinal axis L of the condenser 110 .
- the vertical longitudinally elongated fins 112 and flutes 114 enhance condensation by using surface tension forces to maintain a small liquid film thickness on the condensation surface.
- the fins 112 preferably have a convex surface with a hyperbolic cosine profile to provide a uniform liquid film thickness and maximize condensation; however, other simpler convex curved surfaces that are more easily manufactured can be used with only slightly less performance.
- a convex surface for the fins 112 produces a small liquid film thickness and a concave surface for the flute 114 supports or receives a larger liquid film thickness.
- the convex surfaces of the fins 112 can be drained by concave surfaces of the flutes 114 .
- the flutes 114 serve as drainage channels to keep the condensate from flooding the condensation surfaces.
- the flutes 114 may have a profile that is other than convex such as, but not by way of limitation, generally rectilinear or generally V-shaped.
- the fins 112 and flutes 114 may exist on only the exterior side 116 or interior side 118 of the condenser 110 .
- the condenser 110 may have fins 112 and flutes 114 on the interior and/or the exterior and the condenser 110 is used in conjunction with another condensing device such as another condenser located within the interior 118 and/or around the exterior 116 of the condenser 110 .
- the condenser 110 of the present invention may include fins 112 and flutes 114 on both sides 116 , 118 . Also, heat is conducted axially in the condenser 110 of the present invention.
Abstract
The present invention is directed to a much safer and less expensive way of providing portable oxygen from a gas concentrator for patients who do not want to be tied to a stationary machine or restricted by present oxygen technology. The present invention involves a home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator is condensed into liquid oxygen. The system includes an oxygen concentrator which separates oxygen gas from the ambient air, a condenser in communication with the oxygen concentrator for receiving and liquefying the oxygen gas flow, a cryocooler associated with the condenser, and a first storage dewar in fluid communication with the condenser and adapted to store the oxygen liquefied by the condenser, the first storage dewar including means for transferring liquid oxygen from the first dewar to a second dewar for storing a quantity of oxygen suitable for moveable oxygen treatment.
Description
This application is a continuation-in-part of U.S. patent application Ser. No. 08/876,970, filed Jun. 16, 1997 now U.S. Pat. No. 5,979,440.
The field of this invention relates to using an oxygen concentrator to create a portable supply of supplementary oxygen for ambulatory respiratory patients so that they can lead normal and productive lives—as the typical primary oxygen sources are too bulky to carry or require excessive power to operate.
There is a burgeoning need for home and ambulatory oxygen. Supplemental oxygen is necessary for patients suffering from lung disorders; for example, pulmonary fibrosis, sarcoidosis, or occupational lung disease. For such patients, oxygen therapy is an increasingly beneficial, life-giving development. While not a cure for lung disease, supplemental oxygen increases blood oxygenation, which reverses hypoxemia. This therapy prevents long-term effects of oxygen deficiency on organ systems—in particular, the heart, brain and kidneys. Oxygen treatment is also prescribed for Chronic Obstructive Pulmonary Disease (COPD), which afflicts about 25 million people in the U.S., and for other ailments that weaken the respiratory system, such as heart disease and AIDS. Supplemental oxygen therapy is also prescribed for asthma and emphysema.
The normal prescription for COPD patients requires supplemental oxygen flow via nasal cannula or mask twenty four hours per day. The average patient prescription is two liters per minute of high concentration oxygen to increase the oxygen level of the total air inspired by the patient from the normal 21% to about 40%. While the average oxygen flow requirement is two liters per minute, the average oxygen concentrator has a capacity of four to six liters of oxygen per minute. This extra capacity is occasionally necessary for certain patients who have developed more severe problems but they are not generally able to leave the home (as ambulatory patients) and do not require a portable oxygen supply.
There are currently three modalities for supplemental medical oxygen: high pressure gas cylinders, cryogenic liquid in vacuum insulated containers or thermos bottles commonly called “dewars,” and oxygen concentrators. Some patients require in-home oxygen only while others require in-home as well as ambulatory oxygen depending on their prescription. All three modalities are used for in-home use, although oxygen concentrators are preferred because they do not require dewar refilling or exchange of empty cylinders with full ones.
Only small high pressure gas bottles and small liquid dewars are portable enough to be used for ambulatory needs (outside the home). Either modality may be used for both in-home and ambulatory use or may be combined with an oxygen concentrator which would provide in-home use.
As we describe below, the above-described current methods and apparatus have proven cumbersome and unwieldy and there has been a long-felt need for improved means to supply the demand for portable/ambulatory oxygen.
For people who need to have oxygen but who need to operate away from an oxygen-generating or oxygen-storage source such as a stationary oxygen system (or even a portable system which cannot be easily carried), the two most prescribed options generally available to patients are: (a) to carry with them small cylinders typically in a wheeled stroller; and (b) to carry portable containers typically on a shoulder sling. Both these gaseous oxygen and liquid oxygen options have substantial drawbacks. But from a medical view, both have the ability to increase the productive life of a patient.
The major drawback of the gaseous oxygen option is that the small cylinders of gaseous oxygen can only provide gas for a short duration. Oxygen conserving devices that limit the flow of oxygen to the time of inhalation may be used. However, the conserving devices add to the cost of the service and providers have been reluctant to add it because there often is no health insurance reimbursement. Indeed, the insurance reimbursement for medical oxygen treatment appears to be shrinking.
Another drawback of the gaseous oxygen option is the source of or refill requirement for oxygen once the oxygen has been depleted from the cylinder. These small gas cylinders must be picked up and refilled by the home care provider at a specialized facility. This requires regular visits to a patient's home by a provider and a substantial investment in small cylinders for the provider because so many are left at the patient's home and refilling facility. Although it is technically possible to refill these cylinders in the patient's home using a commercial oxygen concentrator that extracts oxygen from the air, this task would typically require an on-site oxygen compressor to boost the output pressure of the concentrator to a high level in order to fill the cylinders. Additionally, attempting to compress the oxygen in pressurized canisters in the home is dangerous, especially for untrained people. This approach of course presents several safety concerns for in-home use. For example, in order to put enough of this gas in a portable container, it must typically be compressed to high pressure (˜2000 psi). Compressing oxygen from 5 psi (the typical output of an oxygen concentrator) to 2000 psi will produce a large amount of heat. (Enough to raise the temperature 165° C. per stage based on three adiabatic compression stages with intercooling.) This heat, combined with the oxygen which becomes more reactive at higher pressures, sets up a potential combustion hazard in the compressor in the patient's home. Thus, utilizing and storing a high pressure gas system in the patient's home is dangerous and not a practical solution.
The convenience and safety issues are not the only drawbacks of this compressed oxygen approach. Another drawback is that the compressors or pressure boosters needed are costly because they require special care and materials needed for high pressure oxygen compatibility. For example, a Rix Industries, Benicia, Calif., ⅓ hp unit costs about $10,000 while a Haskel International, Burbank, Calif., air-powered booster costs about $2200 in addition to requiring a compressed air supply to drive it. Litton Industries and others also make oxygen pressure boosters.
Turning now to the liquid oxygen storage option, its main drawback is that it requires a base reservoir—a stationary reservoir base unit about the size of a standard beer keg—which has to be refilled about once a week. The liquid oxygen can then be obtained from a base unit and transferred to portable dewars which can be used by ambulatory patients. Also, with the liquid oxygen option, there is substantial waste, as a certain amount of oxygen is lost during the transfer to the portable containers and from evaporation. It is estimated that 20% of the entire contents of the base cylinder will be lost in the course of two weeks because of losses in transfer and normal evaporation. These units will typically boil dry over a period of 30 to 60 days even if no oxygen is withdrawn.
There are other complications. Typically, supplemental oxygen is supplied to the patient by a home care provider, in exchange for which it receives a fixed monetary payment from insurance companies or Medicare regardless of the modality. Oxygen concentrators for use in the home are preferred and are the least expensive option for the home care provider. For outside the home use however, only small high pressure gas bottles and small liquid dewars are portable enough to be used for ambulatory needs. One of these two modalities may be used for both in-home and ambulatory use or may be combined with an oxygen concentrator which would provide in-home use. In either case, the home care provider must make costly weekly or biweekly trips to the patient's home to replenish the oxygen. One of the objects of this invention is to eliminate these costly “milk runs.”
Portable oxygen concentrators are commercially available for providing patients with gaseous oxygen. These devices are “portable” solely in the sense that they can be carried to another point of use such as in an automobile or in an airplane. At present, there are no home oxygen concentrators commercially available that can provide liquid oxygen. One type of medical oxygen concentrator takes in air and passes it through a molecular sieve bed, operating on a pressure swing adsorption cycle, which strips most of the nitrogen out, producing a stream of ˜90% oxygen, for example, as shown in U.S. Pat. Nos. 4,826,510 and 4,971,609 (which are incorporated herein by reference). While, as set out in the Information Disclosure Statement, complex oxygen liquefaction systems have been disclosed for use by the military in jet aircraft, and while large-scale commercial plants have been disclosed, this technology has not yet found its way into the home to help individual patients and to benefit the general public. A truly portable oxygen concentrator has not yet been perfected and this event is unlikely, at least in the near future, because the power requirements are too large to be provided by a lightweight battery pack.
Since liquid oxygen requires periodic delivery and home oxygen concentrators are not commercially available that would create liquid oxygen, there has existed a long-felt need for a device or method having the capability to concentrate oxygen from the air, liquefy it, and transfer it into portable dewars in a home environment, and for a home oxygen concentrator unit which allows excess flow capacity from the concentrator to be stored by either compression or liquefaction for later use.
An aspect of the present invention involves a home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator is condensed into liquid oxygen. The system includes an oxygen concentrator which separates oxygen gas from the ambient air, a condenser in communication with the oxygen concentrator for receiving and liquefying the oxygen gas flow, a cryocooler associated with the condenser, and a first storage dewar in fluid communication with the condenser and adapted to store the oxygen liquefied by the condenser, the first storage dewar including means for transferring liquid oxygen from the first dewar to a second dewar for storing a quantity of oxygen suitable for moveable oxygen treatment.
In an embodiment of the above aspect of the invention, the liquid oxygen transferring means is adapted to increase the pressure in the first dewar.
In a further embodiment of the above aspect of the invention, the liquid transferring means includes a heater immersed within the liquid oxygen in the first dewar.
In a still further embodiment of the above aspect of the invention, the first dewar includes an inner vessel in which the liquid oxygen reside, and liquid transferring means includes a heater attached to the outer surface of inner vessel.
In another embodiment of the above aspect of the invention, the condenser is in communication with the concentrator through a line, and the liquid transferring means includes a compressor located in the line between the condenser and the concentrator.
In an additional embodiment of the above aspect of the invention, the liquid transferring means includes a high-pressure compressor in communication with the concentrator for delivering high-pressure air thereto.
In another embodiment of the above aspect of the invention, the liquid transferring means includes a vaporizer loop associated with the first dewar.
In a further embodiment of the above aspect of the invention, the liquid transferring means includes a controllable heat leak associated with the first dewar.
In a still further embodiment of the above aspect of the invention, the liquid transferring means includes a gravity-assisted dispensing mechanism.
In an additional embodiment of the above aspect of the invention, the system further includes the second storage dewar and the second storage dewar is adapted to be filled at a pressure below 20 psig.
An additional aspect of the invention involves a home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator is condensed into liquid oxygen. The system includes an oxygen concentrator which separates oxygen gas from the ambient air, a condenser in communication with the oxygen concentrator for receiving and liquefying the oxygen gas flow, a cryocooler associated with the condenser, and a portable dewar adapted to interface with the condenser and adapted to store the oxygen liquefied by the condenser.
Another aspect of the present invention involves a method for generating liquid oxygen in a home from a home liquid oxygen ambulatory system having an oxygen concentrator, a condenser, and cryocooler, a storage dewar and means for transferring liquid oxygen from the first dewar to a second dewar. The method includes generating a gaseous supply of oxygen using the oxygen concentrator; splitting off at least a portion of the gaseous supply to be liquefied; cooling the supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen; storing the liquid oxygen in the storage dewar; and transferring the liquid oxygen in the storage dewar with the liquid oxygen transferring means to a second dewar for storing a quantity of liquid oxygen from which smaller quantities can be transferred for moveable oxygen treatment.
In an embodiment of the above aspect of the invention, transferring the liquid oxygen includes increasing the pressure in the first dewar.
In an additional embodiment of the above aspect of the invention, the liquid transferring means includes a heater immersed within the liquid oxygen in the first dewar and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar.
In another embodiment of the above aspect of the invention, the first dewar includes an inner vessel in which the liquid oxygen reside, the liquid transferring means includes a heater attached to the outer surface of inner vessel, and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar.
In a further embodiment of the above aspect of the invention, the condenser is in communication with the concentrator through a line, and the liquid transferring means includes a compressor located in the line between the condenser and the concentrator, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering the condenser and the dewar with the compressor.
In a still further embodiment of the above aspect of the invention, the liquid transferring means includes a high-pressure compressor in communication with the concentrator for delivering high-pressure air thereto, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering the condenser and the dewar with the compressor.
In an additional embodiment of the above aspect of the invention, the liquid transferring means includes a vaporizer loop associated with the first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar with the vaporizer loop so that the pressure is increased in the first dewar.
In another embodiment of the above aspect of the invention, the liquid transferring means includes a controllable heat leak associated with the first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in the first dewar so that the pressure is increased in the first dewar.
In a further embodiment of the above aspect of the invention, the liquid transferring means includes a gravity-assisted dispensing mechanism.
In a still further embodiment of the above aspect of the invention, the system further includes the second storage dewar, the second storage dewar is adapted to filled at a pressure below 20 psig.
Another aspect of the present invention involves a liquefier for a home liquid oxygen ambulatory system that is resistant to plugging. The home liquid oxygen ambulatory system includes an oxygen concentrator for delivering gaseous flow to the liquefier and a storage dewar having an inner vessel for storing liquid oxygen produced by the liquefier. The liquefier includes a condenser, a refrigerating device associated with the condenser, means for communicating incoming gaseous flow from the oxygen concentrator to the condenser, the communicating means having an inner surface with a dimension D, means for venting gaseous flow not condensed from the inner vessel, the venting means having an outer surface with an dimension d, and whereby the dimension D of the inner surface of the communicating means is significantly larger than the dimension d of the outer surface of the venting means to allow for the build-up of solid contaminants on the outer surface of the venting means without plugging up the communicating means.
In an embodiment of the above aspect of the invention, the venting means includes a recuperator comprised of a helical coil of tubing, the tubing having the outer surface with a diameter of the dimension d, whereby the incoming gas stream flows over the outer surface of the helical coil of tubing and a vent stream flows inside the helical coil of tubing.
In another embodiment of the above aspect of the invention, the outer surface of the helical coil of tubing has a cold surface to freeze out trace impurities of solid contaminants such as H2O, CO2 and hydrocarbons.
In a further embodiment of the above aspect of the invention, the communicating means is comprised of a neck tube having the inner surface with a diameter of the dimension D.
In a still further embodiment of the above aspect of the invention, the liquefier further includes a liquid withdrawal tube located central to the refrigerating device, recuperator and condenser for removing liquid oxygen from the storage dewar.
In an additional embodiment of the above aspect of the invention, the refrigerating device is integral with the condenser.
In another embodiment of the above aspect of the invention, the refrigerating device, condenser and recuperator are integral with the storage dewar.
Another aspect of the invention involves a method for generating liquid oxygen in a home from a home liquid oxygen ambulatory system having an oxygen concentrator, a condenser, a cryocooler, a recuperator and a storage dewar. The method includes generating a gaseous supply of oxygen, which includes some trace impurities, using the oxygen concentrator; splitting off at least a portion of the gaseous supply to be liquefied; cooling the supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen; condensing less than all of the gaseous oxygen supply flowing into the condenser; freezing out the trace impurities of the gaseous supply of oxygen and venting the non-condensed nitrogen, argon and oxygen with the recuperator; storing the liquid oxygen in the storage dewar; and periodically removing accumulated frozen impurities on the recuperator by boiling-off any stored liquid oxygen and then flow purging the system until the system has reached room temperature.
Another aspect of the invention involves a generally vertically oriented, gravity assisted condenser for use with a refrigerating device to liquefy gaseous oxygen in a home liquid oxygen ambulatory system. The condenser includes a generally vertically oriented tubular member adapted to conduct heat axially to the refrigerating device, the tubular member having outer and inner surfaces, at least one of the outer and inner surfaces having a plurality of generally vertically oriented flutes and convex fins adapted to increase the condensation rate per unit area by thinning the liquid film and drain the condensate to keep the condensate from flooding the condensation surfaces.
In an embodiment of the above aspect of the invention, the fins have a hyperbolic cosine profile.
In an additional embodiment of the above aspect of the invention, the flutes have a profile selected from the group consisting of concave, generally V-shaped, generally rectilinear.
In another embodiment of the above aspect of the invention, the plurality of generally vertically oriented flutes and convex fins are located on both the outer and inner surfaces.
Another aspect of the invention involves a generally vertically oriented, gravity assisted condenser for use with a refrigerating device to liquefy gaseous oxygen in a home liquid oxygen ambulatory system. The condenser includes a generally vertically oriented tubular member adapted to conduct heat axially to the refrigerating device, the tubular member having outer and inner surfaces, at least one of the outer and inner surfaces includes means for enhancing the condensation rate per unit area by maintaining a small liquid film thickness on the condensation surfaces.
In an embodiment of the above aspect of the invention, the condensation enhancing means includes a plurality of generally vertically oriented flutes and convex fins.
In an additional embodiment of the above aspect of the invention, the fins have a hyperbolic cosine profile.
In a further embodiment of the above aspect of the invention, the flutes have a profile selected from the group consisting of concave, generally V-shaped, generally rectilinear.
In a still further embodiment of the above aspect of the invention, the plurality of generally vertically oriented flutes and convex fins are located on both the outer and inner surfaces.
A flow chart of the preferred embodiment of the invention is set out in FIG. 1 . Its main components include an oxygen concentrator 11, a cryocooler 12, a condenser 13, and a storage/collection dewar or vacuum insulated container 14. In the preferred embodiment, the oxygen concentrator 11 operates on a pressure swing adsorption cycle and essentially strips all or most of the nitrogen from air along with other minor components such as H2O, CO2, CO, NOx, etc. The result is a stream of dry gas with high oxygen concentration (˜92%) flowing in fluid outlet 50. A portion of the gas from this output in fluid outlet 50 is routed to a condenser 13 in association with a cryocooler (or cryogenic refrigerator) 12 through flow lines 51 and 57. The cryocooler provides cooling of the condenser heat exchanger 13 to liquefaction temperatures, causing the oxygen in contact therewith to go from the gaseous to the liquid phase. The condenser 13 typically must be insulated from ambient heating and may in practice even be located inside the dewar 14. In order to lessen the load on the cryocooler 12, a recuperator 15 may be used to pre-cool the incoming stream utilizing the vent flow through line 52 out of the dewar as a cooling medium. In practice, this recuperator 15 may also be located within the dewar 14 to reduce ambient heating.
The controller also provides output indicators for the patient. The liquid level in the dewar is continuously displayed and the patient is alerted when the oxygen concentration is low and when the system is ready for them to transfer liquid to a portable dewar. A modem or wireless link may be included to enable remote monitoring of the key parameters of the system by the home care provider as well as information which is useful for repair, maintenance, billing, and statistical studies of patients for the medical oxygenation market. Key system parameters of interest include the number of liquid transfers performed, the oxygen concentration history, number of run hours on the cryocooler, and time of the last boil-dry as well as number of boil dries performed. The controller may include a computer and/or a microprocessor located either integrally with the liquefaction system claimed herein or remotely therefrom but in communication therewith using either a modem and telephone lines or with a wireless interface. The computer and/or microprocessor may include memory having a database, or may be remotely connected to a memory or database using a network. An Optimal Liquefaction Schedule for optimal operation of the liquefaction system is set out in FIGS. 7-10 and may be stored in the controller using the memory and database. The controller can sense optimum parameters of the system and optimally control, including by activating servomechanisms, liquefaction and transfer of liquid oxygen.
In another embodiment of this system shown in FIG. 2 , the dewar 14 could be eliminated and replaced with a portable dewar 23 which is modified slightly from those existing today. The new portable dewar would interface with the condenser 13, recuperator 15, and controller 16. This embodiment requires a slightly different control scheme from that given for the preferred embodiment as the transfer and boil-dry modes are eliminated. Any small amount of accumulated water and hydrocarbons are eliminated from the portable dewar 23 after each use by allowing it to warm to room temperature before reuse.
In operation, in the preferred embodiment of FIG. 1 , where a pressure swing adsorption (“PSA”) system is used, air is drawn into the oxygen concentrator 11, where it is compressed by an oilless compressor, cooled, and passed through molecular sieve beds operating on the pressure swing adsorption cycle, as shown in U.S. Pat. Nos. 5,366,541; 5,112,367; 5,268,021 and Re. 35,009, which are incorporated herein by reference. This PSA system produces a 5-6 liters per minute (LPM) gas stream with high oxygen concentration at 3-7 pounds per square inch gauge (psig). The composition of this gas stream varies but is typically 90-95% oxygen, 5-6% argon, 0-4% nitrogen, <15 parts per million (ppm) water vapor, and <1 ppm hydrocarbons. Exhaust from the PSA cycle (80-84% nitrogen, 15-19% oxygen, 0.6-0.8% argon, and trace amounts of water vapor, carbon dioxide and hydrocarbons) is vented into the atmosphere as waste gas. In the preferred embodiment, the high concentration oxygen stream in fluid outlet 50 is split with 0-4 lpm going through control valve 24, for patient consumption, and 0.5-1.5 lpm through line 51 and control valve 19 for liquefaction. Oxygen sensor 18, monitors the oxygen concentration produced by oxygen concentrator 11. If the oxygen concentration falls below 88%, controller 16 will close valve 19 and turn off the cryocooler 12.
Even though 88% oxygen is adequate as supplemental oxygen therapy, if this was liquefied, as will be described below, the initial revaporized stream may have a reduced oxygen content because of the close boiling points of the components of the mixture. The temperature of the split gas stream entering the recuperator 15 is about room temperature. It is cooled to about 270 K (or colder) by the vent gas from the dewar flowing through the other side of the recuperator via line 52. The recuperator 15 reduces the load on the cryocooler by using the cold vent gas to pre-cool the oxygen-rich gas stream flowing into the condenser 13. From the recuperator 15 the high oxygen concentration stream flows through a line 57 to the condenser 13, which is cooled to ˜90 K by the cryocooler 12.
The condenser 13 provides cold surfaces to further cool and condense the flow. It is important to note that the gas passing through the condenser 13 is a mixture of oxygen, argon, and nitrogen. The normal boiling points of these components are: 90.18 K, 87.28 K, and 77.36 K respectively. Because of the close boiling points of the components of this mixture, there was initial skepticism because of the concern that all the nitrogen and argon would condense along with the oxygen. If this concern was realized, when this liquid mixture was revaporized, the lower boiling point components; i.e., nitrogen and argon, would boil off first, resulting in flow with high concentrations of nitrogen, argon and a much lower oxygen concentration than that which was supplied to the condenser—which would make the process of oxygen treatment ineffective or a failure.
This concern is explained in FIGS. 3 and 4 which are temperature composition diagrams for binary mixtures of oxygen-argon and oxygen-nitrogen. In these diagrams taken from K. D. Timmerhaus and T. M. Flynn, Cryogenic Process Engineering, Plenum Press, 1989, pp. 296-297, the upper curve at a given pressure defines the dew point and the lower curve defines the bubble point. Looking at FIG. 4 for a pressure of 0.101 MPa, if there is a gas mixture with 10 mole percent nitrogen (point 1), condensation will start when the gas has cooled to the dew point curve (point 2g) which is at a temperature of about 89.5 K in this case. Because oxygen has a higher boiling point than nitrogen, the initial liquid formed (point 2f) will have only 7.4 mole percent nitrogen. If the temperature is lowered to point 3, the liquid will have the composition of point 3f while the remaining vapor will have the composition of point 3g. As the temperature is lowered further to point 4f or below, all of the mixture liquefies and the composition is 10 mole percent nitrogen, the same as at point 1. If this liquid is heated, the nitrogen which has a lower boiling point will vaporize first. Thus, the composition of the first vapor formed will be that of point 4g or about 30 mole percent. As the remaining liquid boils, the mole percent of nitrogen in the vapor drops back to 10 mole percent when point 2g is reached. It is believed that the composition swings with a ternary mixture of oxygen, argon and nitrogen will be even more pronounced than those shown in FIGS. 3 and 4 for binary mixtures. Fortunately, this concern was avoided when the system was set so that only 20 to 99% of the incoming flow to the condenser was actually condensed and when the condenser was controlled in accordance with the parameters as explained herein. This is believed to work because the excess flow operates to purge the vapor with higher impurity concentration from the system and avoid the aforementioned problem. Instead, the results realized were that a high concentration stream of oxygen could be liquefied and stored as set out in the portable ambulatory device claimed herein.
Because of the aforementioned mixture problem, it is important and even critical not to let the amount of argon and nitrogen in the liquid become too high or when it is revaporized, the oxygen concentration will initially be much lower than that conventionally used in supplemental oxygen therapy (>85%). This can be accomplished by selecting the proper condenser temperature, which is a function of pressure, and by not condensing all of the incoming flow. If only part of the incoming flow (20-99%) is liquefied, the remainder of the flow will purge the vapor with higher impurity concentration from the system. A condenser temperature of about 90 K (for ˜17 psia) minimizes the amount of argon and nitrogen liquefied without overly diminishing the yield of oxygen. Hence there will be both liquid and vapor leaving the condenser. The liquid will fall into the dewar 14 and collect. The vapor which has not condensed is vented to the atmosphere through line 52 and the recuperator 15.
The amount of incoming flow liquefied is controlled by setting the mass flow rate relative to the cooling capacity of the cryocooler. The parameters of the condenser and/or cryocooler can be stored in the memory of the controller and/or computer and the controller regulating the incoming flow depending on the parameters stored and/or sensed. Having a mass flow rate which exceeds the cooling capacity of the cryocooler/condenser combination, prevents the incoming flow from being completely liquefied. The mass flow rate is controlled by the amount of flow restriction between inlet valve 19 and flow control valve 25. This includes the flow losses of the valves themselves as well as those in the recuperator, condenser, and all of the interconnecting plumbing.
The pressure in the dewar 14 is maintained slightly above ambient pressure while the cryocooler is operating by valve 25. It is desirable to keep the pressure in the condenser as high as possible because this increases the condensation temperature (as shown in FIGS. 3 and 4 ) which eases the requirements on the cryocooler. Once again this can be controlled by the controller and/or the computer, microprocessor and memory system.
This pressure regulating function of the solenoid on-off valve 25 is accomplished by the pressure transducer 9 and controller 16. Alternately, a back pressure regulating valve (such as a Tescom BB-3 series) or a suitable servomechanism may be used in lieu of the actively controlled solenoid. Liquid keeps accumulating in the dewar 14 until the liquid level sensor 17 signals the controller that the dewar is full or until the oxygen sensor 18 signals that the oxygen concentration of fluid exiting the oxygen concentrator 11 is too low.
In the best mode, operating parameters for optimal operation of the system for the condenser should be that the condenser surface temperature should be in the range from 69.2-109.7 K and pressure should be in the range from 5-65 psia. The gas concentrations into the condenser for medical use should have oxygen in the range of 80-100%, nitrogen from 0-20%, and argon from 0-7%.
In order to transfer liquid from the dewar 14; e.g. to fill a portable LOX dewar 23, the pressure in the dewar 14 must be increased so that liquid can be forced up the dip tube 20. As shown in FIG. 1 , heater 21 is used for this purpose. Heater 21 may be immersed in the liquid oxygen or attached to the outer surface of the inner vessel. The controller 16 ensures that the cryocooler 12 is turned off and valve 25 is closed before the heater 21 is energized. The heater 21 remains turned on until the pressure, measured by pressure transducer 9, reaches about 22 psig.
With reference to FIG. 22 , other alternative means for transferring or dispensing liquid from the dewar 14 will now be described. For simplicity, the alternative liquid transferring means are described with respect to this one Figure. It will be readily apparent to those skilled in the art that any, any combination, or all of the disclosed liquid transferring means discussed below could be used in a single home liquid oxygen ambulatory system.
An alternative means for transferring liquid by raising the pressure in the dewar 14 includes adding a compressor 300 between the oxygen concentrator 11 and the condenser 13. The compressor 300 is preferably added in line 51, either before or after valve 19. The compressor 300 increases the pressure in the storage dewar 14 so that when the portable dewar 23 is engaged, liquid is forced up the dip tube 20 and into the portable dewar 23. An additional benefit of adding a compressor 300 at this location is that it increases the pressure during liquefication in the dewar 14, which increases the saturation temperature. An increased saturation temperature eases the cooling requirements on the cryocooler 12.
A further means for transferring liquid by raising the pressure in the dewar 14 includes using a high-pressure compressor 302 within the oxygen concentrator 11 instead of the typical low-pressure compressor. The high-pressure compressor 302 has the effect of increasing the pressure in the storage dewar 14 so that when the portable dewar 23 is engaged, liquid is forced up the dip tube 20. In addition to easing the cooling requirements on the cryocooler 12, a compressor 302 at this location slightly enhances the PSA cycle.
A still further means for transferring liquid by raising the pressure in the dewar 14 includes using a vaporizer loop 304. In this embodiment, the dewar 14 preferably remains at low pressure while liquid is being produced. When transfer of liquid out of the dewar 14 is desired, a valve 306 is opened to allow some liquid to flow into a coil 308 to be vaporized. This would increase the pressure in the dewar 14 so that liquid could be transferred to the portable dewar 23.
Another means for transferring liquid by raising the pressure in the dewar 14 includes a controllable heat leak such as a conductive strap 310 between ambient and the inner vessel of the dewar 14. When transfer of liquid out of the dewar 14 is desired, the heat leak is controlled so that heat from the ambient is transferred to the liquid, causing it to vaporize. This would increase the pressure in the dewar 14 so that liquid could be transferred to the portable dewar 23.
Another means for transferring liquid by raising the pressure in the dewar 14 includes a controllable pump 312 that is actuated when transfer of liquid out of the dewar 14 is desired.
An additional means for transferring liquid without raising the pressure in the dewar 14 includes incorporating a gravity-assisted dispensing mechanism 314 such as a controllable spigot (analogous to those used to dispense liquids from a large insulated cooler) near the bottom of the dewar 14. Unlike the alternative means for transferring liquid from the storage dewar 14 described above, which expel liquid out of the dip tube 20, the gravity-assisted dispensing mechanism eliminates the need for the dip tube 20. The gravity-assisted dispensing mechanism 314 preferably includes a quick disconnect valve 316 or other flow control means, similar to disconnect valve 22 described above, located on the end of the mechanism 314 to allow for connection of a portable dewar 23.
An additional means for transferring liquid without raising the pressure in the dewar 14 includes incorporating a portable dewar 23 adapted to be filled from a pressure less than 20 psig, which is the standard for currently available home stationary liquid dewars. For example, the portable dewar 23 may be adapted to be filled from a pressure such as 5 psig.
A further means for transferring liquid without raising the pressure in the dewar 14 involves replacing the storage dewar 14 with a specially designed portable dewar 23 such as that described above with respect to FIG. 2 , which interfaces with the rest of the home liquid oxygen ambulatory system.
In order to eliminate accumulation of solid water and hydrocarbons which may be supplied in trace amounts from the oxygen concentrator, the dewar 14, recuperator 15, and condenser 13 will be warmed to room temperature periodically (preferably after about 30 fillings of a portable dewar, or every two months). This procedure is accomplished most economically when the inventory of liquid in the storage dewar is low; e.g. shortly after liquid transfer and a portable dewar has been filled. In this “boil-dry” mode, valve 19 will be closed, the cryocooler 12 is turned-off, valve 25 is open, and heater 21 is energized until all the liquid has boiled-off as evidenced by, for example, the temperature sensor 10 being above 125 K. The heater will boil-off the remaining liquid in the dewar 14 and with it any trace amounts of water and hydrocarbons which are condensed and solidified in the liquid oxygen or on the cold surfaces. Once valve 19 is re-opened, the flow of concentrated oxygen gas purges and removes most of the water vapor and hydrocarbons from the liquefier. The heater 21 will remain turned on until the dewar temperature, measured by temperature sensor 10, has warmed to about 300 K. Any remaining water vapor will be flushed out by gaseous oxygen during the subsequent cooldown.
The dewpoint/frostpoint of the gas stream provided by the oxygen concentrator is below −55° C. Although the mass of water flowing into the liquefier is quite small, the ice/frost formed at such a cold temperature has a very low density and hence, can take a appreciable volume of space that can lead to plugging of the liquefier. Therefore, the design of the recuperator 15 and/or condenser 13 must be able to allow for accumulation of frost without plugging.
With reference to FIG. 19 , an embodiment of a liquefier 70, which is resistant to plugging, will now be described. Elements similar to those previously described are referred to with the reference numerals and are not described in further detail. The liquefier 70 includes an integral coldhead 72, condenser 74 and a recuperator 76 located generally within a dewar 14. Incoming gaseous flow enters a neck tube 78 via an inlet 80 as shown by the arrows. The gaseous flow includes mostly oxygen gas along with a small amount of water vapor and other trace impurities. The gaseous flow is pre-cooled as it passes the helical recuperator 76. Water vapor in the gaseous flow freezes out on surfaces at temperature below its frostpoint such as outer surface 82 of the recuperator 76 and inner surface 84 of the neck tube 78. The neck tube 78 has an inner diameter or dimension D and the helical recuperator 76 is constructed of a tube having an outer diameter or dimension d. By making inner diameter D of the neck tube 78 significantly larger than the outer diameter d of the helical recuperator tube 76 at locations along the neck tube 78 where incoming gaseous flow is present, the liquefier 70 allows for accumulation of frost on the inner surface 84 of the neck tube 78 or outer surface 82 of the recuperator 76 without plugging. This extends the period of time required between boil-dries without causing plugging in the liquefier 70.
Oxygen from the gaseous flow condenses into liquid oxygen at the condenser 74. The condenser 74 is shown in conjunction with a vapor compression cycle cryocooler 86 (evaporator 88, tube-in-tube heat exchanger 90, compressor 92) as its associated refrigerating mechanism. It will be readily understood by those skilled in the art that other refrigerating mechanisms may be used in conjunction with the condenser such as, but not by way of limitation, pulse tube, Stirling, etc. For example, with reference to FIG. 20 , in an alternative embodiment of the invention, a condenser 94 may be used in conjunction with a coldhead 96 from a pulse tube cryocooler 97 to liquefy the incoming flow. The cryocooler 97 includes copper tubes 98, 100 that provide strain relief via respective coils 102, 104. Copper tube 98 connects the coldhead 96 to a compressor 106 and copper tube 100 connects the coldhead 96 to a reservoir volume 108. A flexible copper braid 110 provides a heat conduction path if needed to reject heat from the coldhead 96.
Excess gaseous flow not condensed becomes vent gas that is removed from the liquefier 70 via the recuperator 76. Vent gas enters the recuperator 76 through inlet 112, as shown by the arrows, flows through the helical recuperator 76 (providing the aforementioned pre-cooling) and preferably exits to the atmosphere through outlet 114.
The dewar 14 may include a central liquid withdrawal tube 116 for withdrawing liquid oxygen from the dewar 14. The central liquid withdrawal tube 116 may include an integral liquid level sensor 118 for monitoring the level of the liquid oxygen in the dewar 14. A heater 21 may be attached to the outer surface of the inner vessel of the dewar 14 to assist in transferring liquid oxygen from the dewar 14.
A getter cup 120 such as those used in commercial cryogenic dewars may be attached to the inner vessel of the dewar 14 to maintain a high vacuum in the dewar 14.
At initial start-up or after a periodic boil-dry phase, the dewar, condenser, recuperator, and all associated hardware are at room temperature and must be cooled down. This is accomplished in the “start-up” mode, where valve 19 (see FIG. 1 ) is open, the heater is off, the cryocooler is on, and valve 25 is modulated to control the pressure/flow rate. It is desired to keep the pressure and hence the density of the gas as high as possible while maintaining the flow rate.
The higher density gas will have better heat transfer with the dewar walls and associated hardware. It is noted that higher flow rates will enhance the convection heat transfer but may exceed the cooling capacity. Based on the cooling characteristics of the cryocooler between room temperature and 90 K, the flow rate can be changed to minimize the cool-down time.
The dewar 14 is equipped with at least one relief valve 26 as a safety feature. Another relief valve 29 is provided and in communication with the inlet gas stream 51, before flowing into the recuperator 15. This serves as a back-up for relief valve 26 as well as providing a means to eliminate accumulated water from the recuperator 15 during periods when the cryocooler 12 is off, if valve 25 is closed. A check valve 27 is also provided to prevent backflow into the oxygen concentrator in the event of a malfunction.
For example, FIG. 8 relates to the start-up mode; i.e., when the system is first turned on or after the boil-dry cycle. As shown in FIGS. 6 through 8 and as depicted in FIG. 1 , at start-up mode, the liquid sensor 17 shows zero liquid volume in the dewar and, when the oxygen sensor 18 shows an oxygen concentration greater than 88%, valve 19 is open, heater 21 is off, cryocooler 12 is on, and the indicator or the controller indicates a cool-down state. Valve 25 is modulated to control pressure.
Once the system attains a cool enough temperature, steady state or normal operational condense mode is used. As shown in FIG. 9 , the input to the controller 16 is such that when the oxygen sensor indicates oxygen concentration being greater than 88% and when the other criteria in the left-hand column of FIG. 9 are achieved, the output states set out in the right portion of the chart are attained. For example, when the level of the dewar is sensed as being full, the liquid level sensor indicates a level of approximately 100%, causing closure of valves 19 and 25, keeping the heater off, turning the cryocooler off, and having the indicator signal that the dewar is full.
The transfer mode in FIG. 10 is the stage where one can fill the portable thermos bottles or dewars 23 from the main storage dewar 14. The top portion of FIG. 10 , for example, shows controller readouts where, if the liquid sensor indicates a liquid level of less than 20%, then the conclusion is computed that there is not enough liquid to transfer into the portable dewar from the main dewar as shown. When the operator wants to increase the pressure in the storage dewar to force the liquid oxygen into the portable dewar, the heater is activated, and when the pressure sensor indicates that the pressure exceeds 22 psig, as shown on the last line in the left-hand column of FIG. 10 , the heater 21 is then turned off and the controller readout or indicator shows that the transfer of liquid oxygen can be made to the portable dewar. Finally, FIG. 11 indicates the boil-dry mode, with valve 25 open to allow the vapor to escape, and the various parameters relating thereto.
The double inlet pulse tube refrigerator as shown in FIG. 12 is comprised of a pressure oscillator 30, primary heat rejecter 31, regenerator 32, heat acceptor 33, pulse tube 34, orifice rejecter 35, bypass orifice 36, primary orifice 37, and reservoir volume 38. The preferred refrigerant gas in the PTR closed and pressurized circuit is helium but various other gases such as neon or hydrogen could also be used. In operation, the PTR essentially pumps heat accepted at low temperature in the heat acceptor 33 to the orifice heat rejecter 35 where it is rejected at near ambient temperature. Although FIG. 12 depicts a “U-tube” configuration of the PTR, in-line and coaxial configurations are other possible options. Depicted therein is a piston type pressure oscillator, but other types are possible such as those utilizing diaphragms or bellows.
It is noted that with this type of cryocooler, it may be possible to remove some of the heat from the oxygen stream at a temperature warmer than Tc.
One possible geometry of the generally vertically oriented, gravity assisted condenser 13 in FIG. 1 is shown in FIGS. 14 and 15 . The incoming gas from the oxygen concentrator flows from conduit 57 to chamber 58 and then is distributed through an annular passage 59 between the outer tube 41 and inner rod 42. The inner rod 42 is made of a high thermal conductivity material such as OFHC (Oxygen Free High Conductivity) copper, to minimize the temperature gradient between the surface on which the oxygen condenses (13) and the cryocooler 12. The cold end of the cryocooler is shown by cross-hatched member 61. Due to surface tension, the axial slots or grooves 43 will draw in liquid as it condenses. This will enhance heat transfer from the incoming gas by preventing a liquid film from forming over the entire condenser surface. Condensed liquid will drip off the bottom of the rod 42 while non-condensed gases flow out the end of the annulus 60. It is possible to liquefy all of the incoming flow to the condenser provided the cryocooler has sufficient cooling capacity and temperature capability. However, in order to minimize the amount of nitrogen and argon condensed, the preferred embodiment only condenses between 20-99% of the incoming flow. The incoming flow rate can be determined by the appropriate sizing of flow restrictions downstream of and by controlling valve 19. As mentioned previously, the mass flow rate is chosen to exceed the cooling capacity of the condenser/cryocooler so that only part of the incoming flow is liquefied. Also, the pressure in the condenser is maintained as high as possible while maintaining the desired flow rate. The higher pressure increases the condensation temperature which in turn reduces the requirements on the cryocooler.
In an alternative embodiment of the invention, the flutes 114 may have a profile that is other than convex such as, but not by way of limitation, generally rectilinear or generally V-shaped.
In a further embodiment of the invention, the fins 112 and flutes 114 may exist on only the exterior side 116 or interior side 118 of the condenser 110. Alternatively, the condenser 110 may have fins 112 and flutes 114 on the interior and/or the exterior and the condenser 110 is used in conjunction with another condensing device such as another condenser located within the interior 118 and/or around the exterior 116 of the condenser 110.
Prior art (U.S. Pat. Nos. 4,253,519, 4,216,819) has been limited to horizontal externally fluted tubes with purely radial conduction through the tube wall. In contrast, the condenser 110 of the present invention may include fins 112 and flutes 114 on both sides 116, 118. Also, heat is conducted axially in the condenser 110 of the present invention.
Thus, an improved home/ambulatory liquid oxygen system is disclosed. While the embodiments and applications of this invention have been shown and described, and while the best mode contemplated at the present time by the inventors has been described, it should be apparent to those skilled in the art that many more modifications are possible, including with regard to scaled-up industrial applications, without departing from the inventive concepts therein. Both product and process claims have been included and in the process claims it is understood that the sequence of some of the claims can vary and still be within the scope of this invention. The invention therefore can be expanded, and is not to be restricted except as defined in the appended claims and reasonable equivalence departing therefrom.
Claims (76)
1. A home liquid oxygen ambulatory system for supplying a portable supply of oxygen, where a portion of the gaseous oxygen output obtained from an oxygen concentrator a pressure swing adsorption system is condensed into liquid oxygen, comprising:
(a) an oxygen concentrator a pressure swing adsorption system comprising a molecular sieve bed which separates oxygen gas from receives the ambient air as an input and provides an output of oxygen-enriched gas;
(b) a condenser in communication with said oxygen concentrator pressure swing adsorption system for receiving and liquefying the oxygen gas flow the output from the pressure swing adsorption system;
(c) a cryocooler associated with said condenser; and
(d) a first storage dewar in fluid communication with said condenser and adapted to store the oxygen liquefied by the condenser, the first storage dewar including means for transferring liquid oxygen from the first dewar to a second dewar for storing a quantity of oxygen suitable for moveable oxygen treatment, wherein said liquid oxygen transferring means is adapted to increase the pressure in said first dewar.
2. The system of claim 1 , wherein said liquid transferring means includes a heater immersed within the liquid oxygen in said first dewar.
3. The system of claim 1 , wherein said first dewar includes an inner vessel in which said liquid oxygen reside, and liquid transferring means includes a heater attached to the outer surface of inner vessel.
4. The system of claim 1 , wherein said condenser is in communication with said concentrator pressure swing adsorption system through a line, and said liquid transferring means includes a compressor located in said line between said condenser and said concentrator pressure swing adsorption system.
5. The system of claim 1 , wherein said liquid transferring means includes a high-pressure compressor in communication with said concentrator for delivering high-pressure air thereto.
6. The system of claim 1 , wherein said liquid transferring means includes a vaporizer loop associated with said first dewar.
7. The system of claim 1 , wherein said liquid transferring means includes a controllable heat leak associated with said first dewar.
8. The system of claim 1 , wherein said liquid transferring means includes a gravity-assisted dispensing mechanism.
9. The system of claim 1 , wherein said system further includes said second storage dewar and said second storage dewar is adapted to be filled at a pressure below 20 psig.
10. A method for generating liquid oxygen in a home from a home liquid oxygen ambulatory system having an oxygen concentrator a pressure swing adsorption system comprising a molecular sieve bed, a condenser, and cryocooler, a storage dewar and means for transferring liquid oxygen from the first dewar to a second dewar, comprising:
(a) generating a gaseous supply of oxygen using the oxygen concentrator pressure swing adsorption system which receives the ambient air as an input and provides an output of oxygen-enriched gas;
(b) splitting off at least a portion of the gaseous supply to be liquefied;
(c) cooling said supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen;
(d) storing the liquid oxygen in the storage dewar;
(e) transferring the liquid oxygen in the storage dewar with the liquid oxygen transferring means to a second dewar by increasing the pressure in said first dewar for storing a quantity of liquid oxygen from which smaller quantities can be transferred for moveable oxygen treatment.
11. The method of claim 10 , wherein said liquid transferring means includes a heater immersed within the liquid oxygen in said first dewar and transferring the liquid oxygen includes heating the liquid oxygen in said first dewar so that the pressure is increased in said first dewar.
12. The method of claim 10 , wherein said first dewar includes an inner vessel in which said liquid oxygen reside, said liquid transferring means includes a heater attached to the outer surface of inner vessel, and transferring the liquid oxygen includes heating the liquid oxygen in said first dewar so that the pressure is increased in said first dewar.
13. The method of claim 10 , wherein said condenser is in communication with said concentrator pressure swing adsorption system through a line, and said liquid transferring means includes a compressor located in said line between said condenser and said concentrator pressure swing adsorption system, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering said condenser and said dewar with said compressor.
14. The method of claim 10 , wherein said liquid transferring means includes a high-pressure compressor in communication with said concentrator for delivering high-pressure air thereto, and transferring the liquid oxygen includes increasing the pressure of gaseous oxygen entering said condenser and said dewar with said compressor.
15. The method of claim 10 , wherein said liquid transferring means includes a vaporizer loop associated with said first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in said first dewar with said vaporizer loop so that the pressure is increased in said first dewar.
16. The method of claim 10 , wherein said liquid transferring means includes a controllable heat leak associated with said first dewar, and transferring the liquid oxygen includes heating the liquid oxygen in said first dewar so that the pressure is increased in said first dewar.
17. The method of claim 10 , wherein said liquid transferring means includes a gravity-assisted dispensing mechanism.
18. The method of claim 10 , wherein said system further includes said second storage dewar, said second storage dewar is adapted to filled at a pressure below 20 psig.
19. A liquefier for a home liquid oxygen ambulatory system that is resistant to plugging, the home liquid oxygen ambulatory system having an oxygen concentrator a pressure swing adsorption system comprising a molecular sieve bed for delivering gaseous flow to the liquefier and a storage dewar having an inner vessel for storing liquid oxygen produced by the liquefier, comprising:
a condenser;
a refrigerating mechanism associated with said condenser;
means for communicating incoming gaseous flow from the oxygen concentrator pressure swing adsorption system which receives the ambient air as an input and provides an output of oxygen-enriched gas to the condenser, said communicating means having an inner surface with a dimension D;
means for venting gaseous flow not condensed from the inner vessel, said venting means having an outer surface with a dimension d and disposed within said communicating means; and
whereby the dimension D of the inner surface of the communicating means is significantly larger than the dimension d of the outer surface of the venting means to allow for the build-up of solid contaminants on the outer surface of the venting means without plugging up the communicating means.
20. The liquefier of claim 19 , wherein said venting means includes a recuperator comprised of a helical coil of tubing, the tubing having said outer surface with a diameter of said dimension d, whereby the incoming gas stream flows over the outer surface of said helical coil of tubing and a vent stream flows inside said helical coil of tubing.
21. The liquefier of claim 20 , wherein said outer surface of said helical coil of tubing has a cold surface to freeze out trace impurities of solid contaminants such as H2O, CO2 and hydrocarbons.
22. The liquefier of claim 19 , wherein said communicating means is comprised of a neck tube having said inner surface with a diameter of said dimension D.
23. The liquefier of claim 19 , wherein refrigerating mechanism is integral with the condenser.
24. The liquefier of claim 19 , wherein the refrigerating mechanism and condenser are integral with said storage dewar.
25. A method for generating liquid oxygen in a home from a home liquid oxygen ambulatory system having an oxygen concentrator a pressure swing adsorption system comprising a molecular sieve bed, a condenser, a cryocooler, a recuperator and a storage dewar, comprising:
(a) generating a gaseous supply of oxygen, which includes some trace impurities, using the oxygen concentrator pressure swing adsorption system which receives the ambient air as an input and provides an output of the gaseous supply of oxygen;
(b) splitting off at least a portion of the gaseous supply to be liquefied;
(c) cooling said supply of oxygen using the condenser and cryocooler to transform the gaseous oxygen to liquid oxygen;
(d) condensing less than all of the gaseous oxygen supply flowing into the condenser;
(e) freezing out the trace impurities of the gaseous supply of oxygen and venting the excess gaseous oxygen with said recuperator;
(f) storing the liquid oxygen in the storage dewar; and
(g) periodically removing accumulated frozen impurities on said recuperator by boiling-off any stored liquid oxygen and then flow purging the system until the system has reached room temperature.
26. A generally vertically oriented, gravity assisted condenser for use with a refrigerating mechanism to liquefy gaseous oxygen in a home liquid oxygen ambulatory system, comprising:
a generally vertically oriented tubular member adapted to conduct heat axially to said refrigerating mechanism, the tubular member having a geometric center and outer and inner surfaces, at least one of said outer and inner surfaces having a plurality of generally vertically oriented flutes and convex fins adapted to increase the condensation rate per unit area by thinning the liquid film and drain the condensate to keep the condensate from flooding the condensation surfaces, wherein the flutes and convex fins are circumferentially spaced with respect to each other and not radially aligned with each other relative to the geometric center of the tubular member.
27. The condenser of claim 26 , wherein the fins have a hyperbolic cosine profile.
28. The condenser of claim 26 , wherein said plurality of generally vertically oriented flutes and convex fins are located on said inner surface.
29. The condenser of claim 26 , wherein said plurality of generally vertically oriented flutes and convex fins are located on both said outer and inner surfaces.
30. A generally vertically oriented, gravity assisted condenser for use with a refrigerating mechanism to liquefy gaseous oxygen in a home liquid oxygen ambulatory system, comprising:
a generally vertically oriented tubular member adapted to conduct heat axially to said refrigerating mechanism, the tubular member having outer and inner surfaces, at least one of said outer and inner surfaces includes means for enhancing the condensation rate per unit area by maintaining a small liquid film thickness on the condensation surfaces, said condensation enhancing means including a plurality of generally vertically oriented flutes and convex fins located on both said outer and inner surfaces.
31. An apparatus for supplying oxygen-enriched gas to a patient in a home environment and for use in an ambulatory environment, comprising:
a compressor adapted to receive ambient air and produce compressed air;
a pressure swing adsorption system comprising a molecular sieve bed adapted to produce oxygen-enriched gas, the pressure swing adsorption system having an inlet adapted to receive the compressed air from the compressor and an outlet adapted to provide the oxygen-enriched gas;
a first outlet flow line operatively coupled to the outlet and adapted to deliver a first portion of the oxygen-enriched gas to a patient;
a second outlet flow line operatively coupled to the outlet and adapted to deliver a second portion of the oxygen-enriched gas to a storage vessel; and
a valve positioned and operable to terminate the delivery of the second portion of the oxygen-enriched gas to the storage vessel responsive to an oxygen concentration of the oxygen-enriched gas being below a predetermined value, wherein the first outlet flow line remains substantially unimpeded so as to maintain the delivery of the first portion of the oxygen-enriched gas to the patient even during termination of the second portion of the oxygen-enriched gas to the storage vessel.
32. The apparatus of claim 31, wherein an oxygen concentration of the first portion of the oxygen-enriched gas is at least 80%.
33. The apparatus of claim 31, further comprising an oxygen sensor adapted to sense a concentration of oxygen-enriched gas produced by the pressure swing adsorption system, wherein the valve closes to prevent delivery of the second portion of the oxygen-enriched gas to the storage vessel responsive to the oxygen sensor sensing that the oxygen concentration of the oxygen-enriched gas is below the predetermined value.
34. The apparatus of claim 33, wherein the predetermined value is 88%.
35. The apparatus of claim 33, wherein the oxygen sensor is operatively coupled to the second outlet flow line.
36. The apparatus of claim 31, wherein the valve is positioned between the outlet of the pressure swing adsorption system and the storage vessel.
37. The apparatus of claim 31, further comprising a third outlet flow line having (a) a first end operatively coupled to the outlet of the pressure swing adsorption system, and (b) a second end, wherein the first outlet flow line and the second outlet flow line are coupled to a second end of the third outlet flow line.
38. The apparatus of claim 31, further comprising a product storage tank adapted to receive the oxygen-enriched gas from the pressure swing adsorption system, and wherein an outlet of the product tank corresponds to the outlet of the pressure swing adsorption system.
39. The apparatus of claim 31, wherein the pressure swing adsorption system is an oxygen concentrator.
40. The apparatus of claim 31, further comprising a liquefier adapted to liquefy at least a portion the second portion of the oxygen-enriched gas, and wherein the storage vessel stores the liquefied oxygen.
41. A process for supplying oxygen-enriched gas to a patient and to a storage vessel comprising the steps of:
generating an oxygen product utilizing a pressure swing adsorption system comprising a molecular sieve bed;
directing a first portion of the oxygen product to a patient;
directing a second portion of the oxygen product to a storage vessel;
monitoring an oxygen concentration of the oxygen product; and
interrupting delivery of the second portion of the oxygen product to the storage vessel responsive to the oxygen concentration being below a predetermined value, wherein directing the first portion of the oxygen product to the patient continues while the delivery of the second portion of the oxygen product is interrupted.
42. The process of claim 41, wherein the oxygen product is an oxygen-enriched gas.
43. The process of claim 41, wherein the predetermined value is 88%.
44. The process of claim 41, further comprising:
liquefying at least a portion of the second portion of the oxygen product directed to the storage vessel; and
storing the liquefied oxygen product in the storage vessel.
45. The process of claim 41, further including the step of pressurizing the second portion of the oxygen product directed to the storage vessel to a pressure greater than the pressure of the first portion of the oxygen product directed to the patient.
46. The process of claim 41, wherein the pressure swing adsorption system is an oxygen concentrator.
47. The process of claim 41, further including the step of transferring the oxygen product from the storage vessel to a portable storage vessel.
48. An apparatus for providing oxygen-enriched gas to a patient in a home environment and an ambulatory environment comprising:
a pressure swing adsorption system comprising a molecular sieve bed adapted to generate oxygen-enriched gas;
a first outlet flow line operatively coupled to the pressure swing adsorption system to direct a first portion of the oxygen-enriched gas from the pressure swing adsorption system to a patient;
a storage vessel;
a second outlet flow line operatively coupled to the pressure swing adsorption system to direct a second portion of the oxygen-enriched gas from the pressure swing adsorption system to the storage vessel;
a compressor in fluid communication with the second outlet flow line, wherein the compressor is adapted to compress the second portion of oxygen-enriched gas prior to delivery to the storage vessel; and
a coupling operatively coupled to the storage vessel, wherein the coupling is adapted to be connected with a portable tank to enable filling of the portable tank from the storage vessel.
49. The apparatus of claim 48, further comprising a liquefier adapted to liquefy at least a portion of the second portion of the oxygen-enriched gas directed to the storage vessel, and wherein the storage vessel stores the liquefied oxygen.
50. That apparatus of claim 48, wherein the pressure swing adsorption system is an oxygen concentrator.
51. A process for supplying oxygen-enriched gas to a patient and to a portable storage container comprising the steps of:
generating an oxygen product utilizing a pressure swing adsorption system comprising a molecular sieve bed;
directing a first portion of the oxygen product to a patient;
directing a second portion of the oxygen product to a storage vessel; and
filling a portable storage container with a content of the storage vessel.
52. The process of claim 51, wherein the oxygen product is an oxygen-enriched gas.
53. The process of claim 51, further comprising:
liquefying at least a portion the second portion of the oxygen product directed to the storage vessel; and
storing the liquefied oxygen product in the storage vessel, and wherein filling the portable storage container includes providing the liquefied oxygen product as the content from the storage vessel to the portable storage container.
54. The process of claim 51, wherein the pressure swing adsorption system is an oxygen concentrator.
55. The process of claim 51, wherein the first portion of oxygen product is delivered simultaneously to the patient while the second portion of oxygen product is directed to the storage vessel.
56. The process of claim 55, wherein the flow of the second portion of oxygen product is terminated if the oxygen product is measured to be below a predetermined concentration level.
57. The process of claim 56, wherein the predetermined concentration level is 88%.
58. An apparatus for filling a portable tank with an oxygen product, comprising:
a pressure swing adsorption system comprising a molecular sieve bed adapted to generate oxygen-enriched gas;
a storage vessel;
an outlet flow line operatively coupled to the pressure swing adsorption system to direct at least a portion of the oxygen-enriched gas from the pressure swing adsorption system to the storage vessel;
a compressor to receive the oxygen-enriched gas from the pressure swing adsorption system from the outlet flow line, wherein the compressor is adapted to compress the portion of the oxygen-enriched gas prior to delivery to the storage vessel; and
a coupling operatively coupled to the storage vessel, wherein the coupling is adapted to be connected with a portable tank suitable for human transport to enable filling of the portable tank with a content from the storage vessel.
59. The apparatus of claim 58, further comprising a liquefier adapted to liquefy at least a portion the oxygen-enriched gas directed to the storage vessel, and wherein the storage vessel stores the liquefied oxygen.
60. The apparatus of claim 58, wherein the pressure swing adsorption system is an oxygen concentrator.
61. A method of filling a portable tank for portable transport by a patient with an oxygen product, the method comprising the steps of:
generating an oxygen product gas utilizing a pressure swing adsorption system comprising a molecular sieve bed which receives the ambient air as an input and provides an output of the oxygen product gas at a first pressure;
pressurizing the oxygen product gas to a second pressure subsequent to the generation, the second pressure being greater than the first pressure;
directing the oxygen product at the second pressure to a storage vessel; and
filling a portable tank of sufficient size for portability by a patient with a content of the storage vessel.
62. The method of claim 61, further comprising:
liquefying at least a portion the oxygen product after the compressing step; and
storing the liquefied oxygen product in the storage vessel, and wherein filing the portable tank includes providing the liquefied oxygen product as the content from the storage vessel to the portable tank.
63. The method of claim 61, wherein the pressure swing adsorption system is an oxygen concentrator.
64. The method of claim 61 further including monitoring a purity of the oxygen product and terminating the direction of oxygen product to the storage vessel responsive to the purity being below a predetermined level.
65. A method of producing and storing liquid oxygen in an oxygen patient's residence, comprising:
providing a liquid oxygen producing apparatus;
placing the liquid oxygen producing apparatus in a location at which a user of liquid oxygen resides;
producing liquid oxygen at the location utilizing a pressure swing adsorption system comprising a molecular sieve bed which receives the ambient air as an input and provides an output of oxygen-enriched gas; and
delivering oxygen-enriched gas produced by the pressure swing adsorption system to a patient.
66. The method of claim 65, further including monitoring a purity of the oxygen-enriched gas to determine whether a level of purity is suitable for human consumption.
67. The method of claim 65, wherein the delivering step is conducted while the liquid oxygen producing apparatus is producing the liquid oxygen.
68. The method of claim 65, wherein producing the liquid oxygen is terminated responsive to an oxygen concentration level of the oxygen-enriched gas produced by the pressure swing adsorption system being below a predetermined level.
69. The method of claim 65, further comprising storing the liquid oxygen in a dewar and transferring the liquid oxygen from the dewar to a portable storage device.
70. A home liquid oxygen ambulatory system for supplying an ambulatory portable supply of oxygen comprising:
a pressure swing adsorption system comprising a molecular sieve bed adapted to separate oxygen from ambient air for human consumption;
a liquefier adapted to receive oxygen from the pressure swing adsorption system and liquefying the oxygen;
a first storage dewar in fluid communication with the liquefier and adapted to store oxygen liquefied by the liquefier;
a second portable storage dewar adapted to store a quantity of oxygen suitable for ambulatory moveable oxygen treatment;
a monitor for measuring an oxygen concentration of oxygen from the pressure swing adsorption system; and
a controller receiving signals from the monitor, and adapted to terminate the liquefying of the oxygen responsive to the oxygen concentration being below a predetermined level.
71. The apparatus of claim 70, wherein the predetermined level of oxygen concentration is at least 88% oxygen purity.
72. The apparatus of claim 70, further including a pressure inducer adapted to increase the pressure within the first dewar for facilitating in the transfer of liquid oxygen from the first dewar to the second portable dewar.
73. The apparatus of claim 70, further comprising a flow line from the pressure swing adsorption system to a person so as to deliver oxygen from the pressure swing adsorption system to a patient simultaneous to the delivery of oxygen to the liquefier.
74. The apparatus of claim 70 including a valve operationally controlled by the controller, wherein the valve terminates the flow of oxygen to the liquefier responsive to the oxygen concentration being below a predetermined level.
75. A method for generating liquid oxygen in a home comprising:
generating a gaseous supply of oxygen for human consumption using a pressure swing adsorption system comprising a molecular sieve bed which receives the ambient air as an input and provides an output of the gaseous supply of oxygen;
monitoring a purity of the gaseous oxygen supply to determine if the level of purity is suitable for human consumption;
liquefying the gaseous supply of oxygen responsive to the level of purity being above a predetermined level;
storing the liquid oxygen in a first storage dewar;
transferring the liquid oxygen in the first storage dewar to a portable second storage.
76. The method of claim 75, wherein at least a portion of the gaseous supply of oxygen from the pressure swing adsorption system is delivered to a person for consumption.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/366,986 USRE43398E1 (en) | 1997-06-16 | 2006-03-01 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/876,970 US5979440A (en) | 1997-06-16 | 1997-06-16 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/420,892 US6698423B1 (en) | 1997-06-16 | 1999-10-19 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US11/366,986 USRE43398E1 (en) | 1997-06-16 | 2006-03-01 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/420,892 Reissue US6698423B1 (en) | 1997-06-16 | 1999-10-19 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
Publications (1)
Publication Number | Publication Date |
---|---|
USRE43398E1 true USRE43398E1 (en) | 2012-05-22 |
Family
ID=25368984
Family Applications (5)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US08/876,970 Expired - Lifetime US5979440A (en) | 1997-06-16 | 1997-06-16 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/343,149 Expired - Lifetime US6681764B1 (en) | 1997-06-16 | 1999-06-29 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/342,890 Expired - Lifetime US6651653B1 (en) | 1997-06-16 | 1999-06-29 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/420,892 Ceased US6698423B1 (en) | 1997-06-16 | 1999-10-19 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US11/366,986 Expired - Lifetime USRE43398E1 (en) | 1997-06-16 | 2006-03-01 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
Family Applications Before (4)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US08/876,970 Expired - Lifetime US5979440A (en) | 1997-06-16 | 1997-06-16 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/343,149 Expired - Lifetime US6681764B1 (en) | 1997-06-16 | 1999-06-29 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/342,890 Expired - Lifetime US6651653B1 (en) | 1997-06-16 | 1999-06-29 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US09/420,892 Ceased US6698423B1 (en) | 1997-06-16 | 1999-10-19 | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
Country Status (7)
Country | Link |
---|---|
US (5) | US5979440A (en) |
EP (1) | EP0990107B1 (en) |
JP (2) | JP4183760B2 (en) |
AT (1) | ATE200349T1 (en) |
CA (1) | CA2293287C (en) |
DE (1) | DE69800669T2 (en) |
WO (1) | WO1998058219A1 (en) |
Cited By (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20110239698A1 (en) * | 2008-12-22 | 2011-10-06 | Koninklijke Philips Electronics, N.V. | Liquid oxygen production device and method |
US20130068220A1 (en) * | 2008-09-23 | 2013-03-21 | Ravikumar V. Kudaravalli | Systems and methods for generating liquid oxygen for portable use |
US8418691B2 (en) | 2009-03-20 | 2013-04-16 | Covidien Lp | Leak-compensated pressure regulated volume control ventilation |
US8424521B2 (en) | 2009-02-27 | 2013-04-23 | Covidien Lp | Leak-compensated respiratory mechanics estimation in medical ventilators |
US8434480B2 (en) | 2008-03-31 | 2013-05-07 | Covidien Lp | Ventilator leak compensation |
US8448641B2 (en) | 2009-03-20 | 2013-05-28 | Covidien Lp | Leak-compensated proportional assist ventilation |
US8746248B2 (en) | 2008-03-31 | 2014-06-10 | Covidien Lp | Determination of patient circuit disconnect in leak-compensated ventilatory support |
US8770199B2 (en) | 2012-12-04 | 2014-07-08 | Ino Therapeutics Llc | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US20160003525A1 (en) * | 2009-09-29 | 2016-01-07 | Koninklijke Philips N.V. | System and method for liquefying a fluid and storing the liquefied fluid |
US20170120085A1 (en) * | 2015-10-30 | 2017-05-04 | Richard Givens | Oxygen concentrating self-rescuer device |
US9675771B2 (en) | 2013-10-18 | 2017-06-13 | Covidien Lp | Methods and systems for leak estimation |
US9795756B2 (en) | 2012-12-04 | 2017-10-24 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US10207069B2 (en) | 2008-03-31 | 2019-02-19 | Covidien Lp | System and method for determining ventilator leakage during stable periods within a breath |
US11833297B2 (en) | 2011-12-31 | 2023-12-05 | Covidien Lp | Methods and systems for adaptive base flow and leak compensation |
US11873757B1 (en) | 2022-05-24 | 2024-01-16 | Ray E. Combs | System for delivering oxygen to an internal combustion engine of a vehicle |
Families Citing this family (160)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
ATE235280T1 (en) * | 1994-10-14 | 2003-04-15 | Bird Products Corp | PORTABLE, MECHANICAL AND DRIVEN COMPRESSOR VENTILATOR |
US6024089A (en) | 1997-03-14 | 2000-02-15 | Nelcor Puritan Bennett Incorporated | System and method for setting and displaying ventilator alarms |
US5979440A (en) * | 1997-06-16 | 1999-11-09 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US6347627B1 (en) * | 1998-04-23 | 2002-02-19 | Pioneer Inventions, Inc. | Nitrous oxide based oxygen supply system |
US6446630B1 (en) * | 1999-02-11 | 2002-09-10 | Sunrise Medical Hhg Inc | Cylinder filling medical oxygen concentrator |
FR2792210B1 (en) * | 1999-04-13 | 2001-09-14 | Air Liquide Sante Int | PORTABLE MEDICAL EQUIPMENT FOR OXYGEN THERAPY AT HOME |
US6575159B1 (en) | 1999-10-29 | 2003-06-10 | Mallinckrodt Inc. | Portable liquid oxygen unit with multiple operational orientations |
US6742517B1 (en) | 1999-10-29 | 2004-06-01 | Mallinckrodt, Inc. | High efficiency liquid oxygen system |
DE60043450D1 (en) * | 1999-10-29 | 2010-01-14 | Mallinckrodt Inc | LIQUID OXYGEN CONTAINER AND SUPPLY SYSTEM WITH HIGH EFFICIENCY |
DE60031161T2 (en) | 1999-10-29 | 2007-10-25 | Mallinckrodt, Inc. | DISTRIBUTOR FOR USE IN A PORTABLE UNIT FOR LIQUID OXYGEN |
US6212904B1 (en) * | 1999-11-01 | 2001-04-10 | In-X Corporation | Liquid oxygen production |
FR2809329B1 (en) * | 2000-05-25 | 2002-08-16 | Air Liquide | PORTABLE OXYGEN CONCENTRATOR |
US6336331B1 (en) * | 2000-08-01 | 2002-01-08 | Praxair Technology, Inc. | System for operating cryogenic liquid tankage |
US6511526B2 (en) | 2001-01-12 | 2003-01-28 | Vbox, Incorporated | Pressure swing adsorption gas separation method and apparatus |
FR2833188B1 (en) * | 2001-12-06 | 2004-05-21 | Air Liquide | INSTALLATION AND METHOD FOR PRODUCING PRODUCTS USING A FLUID |
JP3726965B2 (en) * | 2002-07-01 | 2005-12-14 | 富士電機システムズ株式会社 | Oxygen production method and apparatus |
US6889508B2 (en) * | 2002-10-02 | 2005-05-10 | The Boc Group, Inc. | High pressure CO2 purification and supply system |
US6904913B2 (en) * | 2002-10-24 | 2005-06-14 | Acoba, Llc | Method and system for delivery of therapeutic gas to a patient and for filling a cylinder |
US6668581B1 (en) * | 2002-10-30 | 2003-12-30 | Praxair Technology, Inc. | Cryogenic system for providing industrial gas to a use point |
US20040197616A1 (en) * | 2003-04-01 | 2004-10-07 | Edlund David J. | Oxidant-enriched fuel cell system |
DE10337138A1 (en) * | 2003-08-11 | 2005-03-17 | Freitag, Lutz, Dr. | Method and arrangement for the respiratory assistance of a patient as well as tracheal prosthesis and catheter |
US7588033B2 (en) | 2003-06-18 | 2009-09-15 | Breathe Technologies, Inc. | Methods, systems and devices for improving ventilation in a lung area |
DE10334516B4 (en) * | 2003-07-29 | 2006-06-14 | Sorin Group Deutschland Gmbh | Display and operating device for medical devices and display / control unit therefor |
AU2004266693B2 (en) | 2003-08-18 | 2011-03-10 | Breathe Technologies, Inc | Method and device for non-invasive ventilation with nasal interface |
US7059138B2 (en) * | 2003-09-23 | 2006-06-13 | Praxair Technology, Inc. | Biological refrigeration system |
US20050072423A1 (en) | 2003-10-07 | 2005-04-07 | Deane Geoffrey Frank | Portable gas fractionalization system |
US7066985B2 (en) | 2003-10-07 | 2006-06-27 | Inogen, Inc. | Portable gas fractionalization system |
US7135059B2 (en) | 2003-10-07 | 2006-11-14 | Inogen, Inc. | Portable gas fractionalization system |
CA2540599C (en) | 2003-10-07 | 2013-09-03 | Inogen, Inc. | Portable gas fractionalization system |
US20050274142A1 (en) * | 2004-06-14 | 2005-12-15 | Corey John A | Cryogenically producing oxygen-enriched liquid and/or gaseous oxygen from atmospheric air |
US7913497B2 (en) * | 2004-07-01 | 2011-03-29 | Respironics, Inc. | Desiccant cartridge |
US7210312B2 (en) * | 2004-08-03 | 2007-05-01 | Sunpower, Inc. | Energy efficient, inexpensive extraction of oxygen from ambient air for portable and home use |
US7213400B2 (en) * | 2004-10-26 | 2007-05-08 | Respironics In-X, Inc. | Liquefying and storing a gas |
US7165422B2 (en) * | 2004-11-08 | 2007-01-23 | Mmr Technologies, Inc. | Small-scale gas liquefier |
US7121906B2 (en) * | 2004-11-30 | 2006-10-17 | Carrier Corporation | Method and apparatus for decreasing marine vessel power plant exhaust temperature |
US20060112693A1 (en) * | 2004-11-30 | 2006-06-01 | Sundel Timothy N | Method and apparatus for power generation using waste heat |
US7665304B2 (en) | 2004-11-30 | 2010-02-23 | Carrier Corporation | Rankine cycle device having multiple turbo-generators |
US7833311B2 (en) * | 2004-12-20 | 2010-11-16 | Idatech, Llc | Temperature-based breakthrough detection and pressure swing adsorption systems and fuel processing systems including the same |
US7393382B2 (en) * | 2004-12-20 | 2008-07-01 | Idatech Llc | Temperature-based breakthrough detection and pressure swing adsorption systems and fuel processing systems including the same |
US7399342B2 (en) * | 2004-12-22 | 2008-07-15 | Idatech, Llc | Systems and methods for regulating heating assembly operation through pressure swing adsorption purge control |
US7093479B2 (en) * | 2005-01-13 | 2006-08-22 | International Business Machines Corporation | Method and apparatus for indicating a parameter of transmitted fluid |
US7900627B2 (en) * | 2005-01-18 | 2011-03-08 | Respironics, Inc. | Trans-fill method and system |
US7604005B2 (en) * | 2005-02-09 | 2009-10-20 | Vbox Incorporated | Adsorbent cartridge for oxygen concentrator |
US8020553B2 (en) * | 2005-02-09 | 2011-09-20 | Vbox, Incorporated | Ambulatory oxygen concentrator containing a three phase vacuum separation system |
US7866315B2 (en) * | 2005-02-09 | 2011-01-11 | Vbox, Incorporated | Method and apparatus for controlling the purity of oxygen produced by an oxygen concentrator |
US7431032B2 (en) * | 2005-02-09 | 2008-10-07 | Vbox Incorporated | Low power ambulatory oxygen concentrator |
US7171963B2 (en) * | 2005-02-09 | 2007-02-06 | Vbox, Incorporated | Product pump for an oxygen concentrator |
US20060174875A1 (en) * | 2005-02-09 | 2006-08-10 | Vbox, Incorporated | Ambulatory oxygen concentrator containing a power pack |
US20060174877A1 (en) * | 2005-02-09 | 2006-08-10 | Vbox, Incorporated | Portable oxygen concentrator with a docking station |
US7954490B2 (en) * | 2005-02-09 | 2011-06-07 | Vbox, Incorporated | Method of providing ambulatory oxygen |
US7121276B2 (en) * | 2005-02-09 | 2006-10-17 | Vbox, Incorporated | Personal oxygen concentrator |
US20060174871A1 (en) * | 2005-02-09 | 2006-08-10 | Vbox, Incorporated | Ambulatory oxygen concentrator with high efficiency adsorbent |
US7766010B2 (en) * | 2005-02-09 | 2010-08-03 | Vbox, Incorporated | Method of controlling the rate of oxygen produced by an oxygen concentrator |
US20060260327A1 (en) * | 2005-05-18 | 2006-11-23 | Shoji Kanamori | Apparatus and method for rapidly freezing small objects |
US20060260358A1 (en) * | 2005-05-18 | 2006-11-23 | Kun Leslie C | Gas separation liquefaction means and processes |
US20070000258A1 (en) * | 2005-07-01 | 2007-01-04 | Bonaquist Dante P | Biological refrigeration sytem |
US7721733B2 (en) * | 2005-07-29 | 2010-05-25 | Ric Investments, Llc | Portable liquid oxygen delivery system |
CN101454041B (en) | 2005-09-20 | 2012-12-12 | 呼吸科技公司 | Systems, methods and apparatus for respiratory support of a patient |
US7686870B1 (en) | 2005-12-29 | 2010-03-30 | Inogen, Inc. | Expandable product rate portable gas fractionalization system |
US7556670B2 (en) * | 2006-03-16 | 2009-07-07 | Aylsworth Alonzo C | Method and system of coordinating an intensifier and sieve beds |
US7459008B2 (en) * | 2006-03-16 | 2008-12-02 | Aylsworth Alonzo C | Method and system of operating a trans-fill device |
US7736132B2 (en) * | 2006-04-03 | 2010-06-15 | Respironics Oxytec, Inc. | Compressors and methods for use |
US8753435B2 (en) * | 2006-04-03 | 2014-06-17 | Ric Investments, Llc | Portable oxygen concentrator |
US9229630B2 (en) * | 2006-04-03 | 2016-01-05 | Respironics Oxytec, Inc | User interface for a portable oxygen concentrator |
US8021310B2 (en) | 2006-04-21 | 2011-09-20 | Nellcor Puritan Bennett Llc | Work of breathing display for a ventilation system |
CN101541365A (en) * | 2006-05-18 | 2009-09-23 | 呼吸科技公司 | Tracheostoma tracheotomy method and device |
JP2009545384A (en) | 2006-08-03 | 2009-12-24 | ブリーズ テクノロジーズ, インコーポレイテッド | Method and apparatus for minimally invasive respiratory assistance |
US7677247B2 (en) * | 2006-08-16 | 2010-03-16 | Rescue Air Systems, Inc | Safety system and method of an underground mine |
WO2008021538A2 (en) * | 2006-08-16 | 2008-02-21 | Rescue Air Systems, Inc. | Breathable air safety system and method having an air storage sub-system |
US7694678B2 (en) * | 2006-08-16 | 2010-04-13 | Rescue Air Systems, Inc. | Breathable air safety system and method having a fill station |
US7673629B2 (en) * | 2006-08-16 | 2010-03-09 | Rescue Air Systems, Inc | Safety system and method of a tunnel structure |
US7621269B2 (en) * | 2006-08-16 | 2009-11-24 | Rescue Air Systems, Inc. | Breathable air safety system and method having at least one fill site |
US8733355B2 (en) * | 2006-08-16 | 2014-05-27 | Rescue Air Systems, Inc. | Breathable air safety system and method |
US7527056B2 (en) * | 2006-08-16 | 2009-05-05 | Rescure Air Systems, Inc. | Breathable air safety system and method having an air storage sub-system |
US7763103B2 (en) | 2006-08-28 | 2010-07-27 | Ric Investments, Llc | Oxygen concentration system |
ATE489048T1 (en) * | 2006-09-08 | 2010-12-15 | Arbel Medical Ltd | DEVICE FOR COMBINED TREATMENT |
US7784461B2 (en) | 2006-09-26 | 2010-08-31 | Nellcor Puritan Bennett Llc | Three-dimensional waveform display for a breathing assistance system |
US20080208181A1 (en) * | 2007-01-19 | 2008-08-28 | Arbel Medical Ltd. | Thermally Insulated Needles For Dermatological Applications |
US8468839B2 (en) * | 2007-01-30 | 2013-06-25 | Ric Investments, Llc | Portable liquid oxygen storage unit |
US8156972B2 (en) * | 2007-04-20 | 2012-04-17 | Ric Investments, Llc | System and method for filling a portable liquified gas storage/delivery system |
WO2008144589A1 (en) | 2007-05-18 | 2008-11-27 | Breathe Technologies, Inc. | Methods and devices for sensing respiration and providing ventilation therapy |
US20100162730A1 (en) * | 2007-06-14 | 2010-07-01 | Arbel Medical Ltd. | Siphon for delivery of liquid cryogen from dewar flask |
WO2009007963A1 (en) * | 2007-07-09 | 2009-01-15 | Arbel Medical Ltd. | Cryosheath |
US20090019886A1 (en) * | 2007-07-20 | 2009-01-22 | Inspired Technologies, Inc. | Method and Apparatus for liquefaction of a Gas |
US20090030381A1 (en) * | 2007-07-23 | 2009-01-29 | Lind Casey J | Arced Hypodermic Needle |
US20090065007A1 (en) | 2007-09-06 | 2009-03-12 | Wilkinson William R | Oxygen concentrator apparatus and method |
CN101873875B (en) | 2007-09-26 | 2014-11-12 | 呼吸科技公司 | Methods and devices for providing inspiratory and expiratory flow relief during ventilation therapy |
CN101888868B (en) | 2007-09-26 | 2014-01-22 | 呼吸科技公司 | Methods and devices for treating sleep apnea |
CN101836028B (en) * | 2007-10-22 | 2012-05-23 | 皇家飞利浦电子股份有限公司 | Liquid to high pressure gas transfill system and method |
US9395046B2 (en) | 2007-10-22 | 2016-07-19 | Koninklijke Philips N.V. | Liquid to high pressure gas transfill system and method |
WO2009066292A1 (en) * | 2007-11-21 | 2009-05-28 | Arbel Medical Ltd. | Pumping unit for delivery of liquid medium from a vessel |
US7837765B2 (en) | 2007-12-12 | 2010-11-23 | Idatech, Llc | Systems and methods for supplying auxiliary fuel streams during intermittent byproduct discharge from pressure swing adsorption assemblies |
US8070841B2 (en) | 2007-12-12 | 2011-12-06 | Idatech, Llc | Systems and methods for supplying auxiliary fuel streams during intermittent byproduct discharge from pressure swing adsorption assemblies |
US8464542B2 (en) * | 2007-12-28 | 2013-06-18 | D-Wave Systems Inc. | Systems, methods, and apparatus for cryogenic refrigeration |
WO2009090647A2 (en) * | 2008-01-15 | 2009-07-23 | Arbel Medical Ltd. | Cryosurgical instrument insulating system |
CN101977656A (en) * | 2008-01-18 | 2011-02-16 | 呼吸科技公司 | Methods and devices for improving efficacy of non-invasive ventilation |
US20090255274A1 (en) * | 2008-04-14 | 2009-10-15 | Ungar Eugene K | System and method for recharging a high pressure gas storage container by transport of a low pressure cryogenic fluid |
US8083733B2 (en) | 2008-04-16 | 2011-12-27 | Icecure Medical Ltd. | Cryosurgical instrument with enhanced heat exchange |
US8776793B2 (en) | 2008-04-18 | 2014-07-15 | Breathe Technologies, Inc. | Methods and devices for sensing respiration and controlling ventilator functions |
US8770193B2 (en) | 2008-04-18 | 2014-07-08 | Breathe Technologies, Inc. | Methods and devices for sensing respiration and controlling ventilator functions |
CA2734296C (en) | 2008-08-22 | 2018-12-18 | Breathe Technologies, Inc. | Methods and devices for providing mechanical ventilation with an open airway interface |
WO2010033373A2 (en) * | 2008-09-18 | 2010-03-25 | Nellcor Puritan Bennett Llc | Compact cryogenic cooling chamber for oxygen liquefaction system |
JP5711661B2 (en) | 2008-10-01 | 2015-05-07 | ブリーズ・テクノロジーズ・インコーポレーテッド | Ventilator with biofeedback monitoring and controls to improve patient activity and health |
US8109295B2 (en) * | 2008-10-24 | 2012-02-07 | Tyco Valves & Controls Lp | Manifold assembly |
US20100281917A1 (en) * | 2008-11-05 | 2010-11-11 | Alexander Levin | Apparatus and Method for Condensing Contaminants for a Cryogenic System |
WO2010115166A1 (en) | 2009-04-02 | 2010-10-07 | Breathe Technologies, Inc. | Methods, systems and devices for non-invasive open ventilation with gas delivery nozzles in free space |
US9132250B2 (en) | 2009-09-03 | 2015-09-15 | Breathe Technologies, Inc. | Methods, systems and devices for non-invasive ventilation including a non-sealing ventilation interface with an entrainment port and/or pressure feature |
US8402965B1 (en) | 2009-01-30 | 2013-03-26 | Essex Cryogenics Of Missouri, Inc. | Mass oxygen distribution system |
US7967814B2 (en) | 2009-02-05 | 2011-06-28 | Icecure Medical Ltd. | Cryoprobe with vibrating mechanism |
WO2010105158A1 (en) * | 2009-03-12 | 2010-09-16 | Icecure Medical Ltd. | Combined cryotherapy and brachytherapy device and method |
US9962512B2 (en) | 2009-04-02 | 2018-05-08 | Breathe Technologies, Inc. | Methods, systems and devices for non-invasive ventilation including a non-sealing ventilation interface with a free space nozzle feature |
KR101030585B1 (en) | 2009-05-11 | 2011-04-21 | 신동옥 | Communication Device having oxygen supply function |
US20100305439A1 (en) * | 2009-05-27 | 2010-12-02 | Eyal Shai | Device and Method for Three-Dimensional Guidance and Three-Dimensional Monitoring of Cryoablation |
US8695600B2 (en) | 2009-07-22 | 2014-04-15 | Vbox, Incorporated | Method of separating and distributing oxygen |
US20110029910A1 (en) * | 2009-07-31 | 2011-02-03 | Nellcor Puritan Bennett Llc | Method And System For Providing A Graphical User Interface For Delivering A Low Flow Recruitment Maneuver |
WO2011029074A1 (en) | 2009-09-03 | 2011-03-10 | Breathe Technologies, Inc. | Methods, systems and devices for non-invasive ventilation including a non-sealing ventilation interface with an entrainment port and/or pressure feature |
RU2012117598A (en) * | 2009-09-28 | 2013-11-20 | Конинклейке Филипс Элекроникс Н.В. | SYSTEM AND METHOD FOR LIQUIDATION AND STORAGE OF A FLUID |
EP2483616A2 (en) * | 2009-09-28 | 2012-08-08 | Koninklijke Philips Electronics N.V. | System and method for liquefying and storing a fluid |
US9119925B2 (en) | 2009-12-04 | 2015-09-01 | Covidien Lp | Quick initiation of respiratory support via a ventilator user interface |
US8924878B2 (en) | 2009-12-04 | 2014-12-30 | Covidien Lp | Display and access to settings on a ventilator graphical user interface |
US8335992B2 (en) | 2009-12-04 | 2012-12-18 | Nellcor Puritan Bennett Llc | Visual indication of settings changes on a ventilator graphical user interface |
US8499252B2 (en) | 2009-12-18 | 2013-07-30 | Covidien Lp | Display of respiratory data graphs on a ventilator graphical user interface |
US9262588B2 (en) | 2009-12-18 | 2016-02-16 | Covidien Lp | Display of respiratory data graphs on a ventilator graphical user interface |
US7967815B1 (en) | 2010-03-25 | 2011-06-28 | Icecure Medical Ltd. | Cryosurgical instrument with enhanced heat transfer |
WO2011117765A2 (en) * | 2010-03-25 | 2011-09-29 | Koninklijke Philips Electronics N.V. | Controlling a oxygen liquefaction system responsive to a disturbance in supplied power |
US7938822B1 (en) | 2010-05-12 | 2011-05-10 | Icecure Medical Ltd. | Heating and cooling of cryosurgical instrument using a single cryogen |
US8080005B1 (en) | 2010-06-10 | 2011-12-20 | Icecure Medical Ltd. | Closed loop cryosurgical pressure and flow regulated system |
CN103096981B (en) * | 2010-08-16 | 2015-07-22 | 呼吸科技公司 | Methods, systems and devices using lox to provide ventilatory support |
US8616207B2 (en) | 2010-09-07 | 2013-12-31 | Inova Labs, Inc. | Oxygen concentrator heat management system and method |
US20120055474A1 (en) | 2010-09-07 | 2012-03-08 | Wilkinson William R | Methods and systems for providing oxygen enriched gas |
US8939152B2 (en) | 2010-09-30 | 2015-01-27 | Breathe Technologies, Inc. | Methods, systems and devices for humidifying a respiratory tract |
CN103857448B (en) | 2011-03-14 | 2016-06-29 | 皇家飞利浦有限公司 | Oxygen concentrator and liquefier system and operational approach thereof |
US8702841B2 (en) * | 2012-04-17 | 2014-04-22 | Inogen, Inc. | Adsorber replacement notification for a portable gas concentrator |
US10362967B2 (en) | 2012-07-09 | 2019-07-30 | Covidien Lp | Systems and methods for missed breath detection and indication |
AU2013328916A1 (en) | 2012-10-12 | 2015-05-14 | Inova Labs, Inc. | Oxygen concentrator systems and methods |
NZ707159A (en) | 2012-10-12 | 2018-06-29 | Inova Labs Inc | Dual oxygen concentrator systems and methods |
WO2014059405A1 (en) | 2012-10-12 | 2014-04-17 | Inova Labs, Inc. | Method and systems for the delivery of oxygen enriched gas |
US9052129B2 (en) * | 2012-11-29 | 2015-06-09 | Luciano Faccin | Charging device for cooling system |
US9517365B2 (en) * | 2013-03-15 | 2016-12-13 | Stephen JUAIRE | Portable oxygen system |
GB2533240B (en) * | 2013-08-02 | 2020-03-11 | Chart Inc | Cryocooler with magnetic reciprocating piston |
US9440179B2 (en) | 2014-02-14 | 2016-09-13 | InovaLabs, LLC | Oxygen concentrator pump systems and methods |
FR3020450B1 (en) * | 2014-04-24 | 2016-05-20 | Air Liquide | LIQUID OXYGEN GENERATOR WITH THERMOELECTRIC COOLANT FOR HOME HEALTH |
WO2016022718A1 (en) | 2014-08-08 | 2016-02-11 | D-Wave Systems Inc. | Systems and methods for electrostatic trapping of contaminants in cryogenic refrigeration systems |
US9950129B2 (en) | 2014-10-27 | 2018-04-24 | Covidien Lp | Ventilation triggering using change-point detection |
US20160184760A1 (en) * | 2014-12-30 | 2016-06-30 | Pacific Consolidated Industries, Llc | Adsorption air separation unit with purge recovery tank |
US9623982B2 (en) * | 2015-01-08 | 2017-04-18 | Airbus Group India Private Limited | On-board aircraft nitrogen enriched air and cooling fluid generation system and method |
US20160201983A1 (en) * | 2015-01-08 | 2016-07-14 | AIRBUS GROUP INDIA PRIVATE LIMllTED | On-board aircraft oxygen enriched air and nitrogen enriched air generation system and method |
US10905836B2 (en) | 2015-04-02 | 2021-02-02 | Hill-Rom Services Pte. Ltd. | Manifold for respiratory device |
FR3035194A1 (en) | 2015-04-16 | 2016-10-21 | Air Liquide | OXYGEN SUPPLY INSTALLATION ASSOCIATING AN OXYGEN CONCENTRATOR WITH AN AUTONOMOUS GAS LIQUEFACTION DEVICE |
WO2017192660A1 (en) | 2016-05-03 | 2017-11-09 | Inova Labs, Inc. | Method and systems for the delivery of oxygen enriched gas |
RU2666594C1 (en) * | 2017-03-28 | 2018-09-11 | Акционерное общество "Ассоциация разработчиков и производителей систем мониторинга" | Method of adaptation and restoration, training and regulating effect on a human organism |
US10792449B2 (en) | 2017-10-03 | 2020-10-06 | Breathe Technologies, Inc. | Patient interface with integrated jet pump |
EP3787725A4 (en) * | 2018-03-24 | 2022-03-23 | Vladimir Belyaev | Methods, systems and apparatuses for supplying breathable gases |
US11535407B1 (en) * | 2019-03-21 | 2022-12-27 | Advanced Cooling Technologies | Thermal management system |
US11624556B2 (en) | 2019-05-06 | 2023-04-11 | Messer Industries Usa, Inc. | Impurity control for a high pressure CO2 purification and supply system |
CN110260148A (en) * | 2019-06-28 | 2019-09-20 | 四川泰博流体科技有限公司 | A kind of storage facilities of liquid air, method and air liquefying apparatus |
US11633224B2 (en) | 2020-02-10 | 2023-04-25 | Icecure Medical Ltd. | Cryogen pump |
US11672934B2 (en) | 2020-05-12 | 2023-06-13 | Covidien Lp | Remote ventilator adjustment |
CA3189540A1 (en) * | 2020-07-16 | 2022-01-20 | Invacare Corporation | System and method for concentrating gas |
CN115228124B (en) * | 2022-08-02 | 2023-05-09 | 安徽扬天金塑新能源装备有限公司 | Vacuum low-temperature gas purification device |
Citations (216)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US609499A (en) * | 1898-08-23 | chatwood | ||
US621536A (en) * | 1899-03-21 | Apparatus for liquefying air | ||
US621537A (en) * | 1899-03-21 | Apparatus for liquefying gas | ||
US665912A (en) * | 1900-01-03 | 1901-01-15 | Emile Jolicard | Boiler. |
US707633A (en) * | 1901-02-15 | 1902-08-26 | James F Place | Art or process of liquefying air or other gases and cooling by means thereof. |
US718572A (en) * | 1902-02-17 | 1903-01-13 | Edwin Joseph Richardson | Apparatus for the liquefaction of air or other aeriform fluids. |
US879302A (en) * | 1905-04-03 | 1908-02-18 | Colorado Iron Works Co | Blast-heating apparatus. |
US881176A (en) * | 1906-02-23 | 1908-03-10 | Georges Claude | Apparatus for the liquefaction of air. |
US948835A (en) * | 1910-02-08 | Bruce Walter | Ammonia-condenser. | |
US1454053A (en) * | 1920-02-18 | 1923-05-08 | Griscom Russell Co | Oil cooler |
US1782409A (en) * | 1927-12-19 | 1930-11-25 | Griscom Russell Co | Heat exchanger |
US1796510A (en) * | 1929-06-17 | 1931-03-17 | Delas Francois Xavier J Albert | Surface condenser and the like |
US1821080A (en) * | 1930-10-15 | 1931-09-01 | Engineering Products Corp Inc | Radiator |
US1867163A (en) * | 1925-01-26 | 1932-07-12 | Louis Chavanne J | Heat recuperation |
USRE19031E (en) | 1926-12-29 | 1933-12-19 | Process and apparatus for the | |
US1957006A (en) * | 1927-04-27 | 1934-05-01 | Sulphide Corp | Method of and apparatus for condensing sulphur |
US2017676A (en) * | 1933-03-11 | 1935-10-15 | American Lurgi Corp | Method of and apparatus for condensing sulphuric acid |
US2194654A (en) * | 1936-05-12 | 1940-03-26 | Hadamovsky Paul | Apparatus for liquefying gases |
US2210031A (en) * | 1936-08-28 | 1940-08-06 | Pfaudler Co Inc | Refrigerating apparatus and method |
US2318206A (en) * | 1940-06-17 | 1943-05-04 | M Werk Company | Apparatus for treating liquids flowing through heated tubes |
US2384714A (en) * | 1943-04-12 | 1945-09-11 | Tech Studien Ag | Tubular heat exchanger |
US2434519A (en) * | 1942-04-18 | 1948-01-13 | Raskin Walter | Heat exchange conduit with a spiral fin having a capillary groove |
US2440245A (en) * | 1944-03-13 | 1948-04-27 | Standard Telephones Cables Ltd | Cooling of high-temperature bodies |
US2751199A (en) * | 1951-04-18 | 1956-06-19 | Taco Heaters Inc | Heat exchanger |
US2797554A (en) * | 1954-01-06 | 1957-07-02 | William J Donovan | Heat exchanger in refrigeration system |
US2905447A (en) * | 1956-05-04 | 1959-09-22 | Huet Andre | Tubular heat-exchanger |
US2909903A (en) | 1956-11-07 | 1959-10-27 | Little Inc A | Liquefaction of low-boiling gases |
US2919555A (en) | 1955-07-28 | 1960-01-05 | Joy Mfg Co | Apparatus for and method of separating gases |
US2937079A (en) * | 1956-08-06 | 1960-05-17 | Phillips Petroleum Co | Apparatus for contacting and subsequently separating immiscible liquids |
US2943454A (en) * | 1958-06-30 | 1960-07-05 | Mine Safety Appliances Co | Liquid oxygen converter |
US2944627A (en) | 1958-02-12 | 1960-07-12 | Exxon Research Engineering Co | Method and apparatus for fractionating gaseous mixtures by adsorption |
US2945354A (en) * | 1957-03-18 | 1960-07-19 | North American Aviation Inc | Liquid oxygen conversion system |
US2958204A (en) * | 1956-08-13 | 1960-11-01 | Aro Equipment Corp | Liquid oxygen converter |
US2960834A (en) * | 1954-11-22 | 1960-11-22 | Garrett Corp | Production of liquid oxygen from atmospheric air |
US2964919A (en) * | 1958-07-07 | 1960-12-20 | British Oxygen Co Ltd | Converter system for liquefied gases |
US2969957A (en) * | 1956-01-10 | 1961-01-31 | Thomson Houston Comp Francaise | Electric discharge device cooling systems |
US2970452A (en) * | 1959-04-01 | 1961-02-07 | Union Carbide Corp | Method and apparatus for supplying liquefied gas |
US2993682A (en) * | 1957-03-18 | 1961-07-25 | Huet Andre | Heat exchanger tubes |
US3055643A (en) * | 1956-08-06 | 1962-09-25 | Thomson Houston Comp Francaise | Heat exchangers |
US3097497A (en) | 1959-08-14 | 1963-07-16 | Normalair Ltd | Oxygen supply systems |
US3117426A (en) * | 1960-11-23 | 1964-01-14 | Garrett Corp | Environmental system for protective suit |
US3152589A (en) * | 1959-04-16 | 1964-10-13 | British Oxygen Co Ltd | Liquid oxygen system for passenger aircraft |
US3183678A (en) * | 1963-04-29 | 1965-05-18 | Bendix Corp | Liquid to gas conversion system |
US3186406A (en) * | 1959-02-21 | 1965-06-01 | Normalair Ltd | Breathing apparatus |
US3199303A (en) * | 1963-05-09 | 1965-08-10 | Union Carbide Corp | Oxygen therapy system |
US3205670A (en) * | 1962-09-24 | 1965-09-14 | Puritan Compressed Gas Corp | Oxygen supply system |
US3313091A (en) | 1963-11-04 | 1967-04-11 | Exxon Research Engineering Co | Vacuum cycle adsorption |
US3318307A (en) | 1964-08-03 | 1967-05-09 | Firewel Company Inc | Breathing pack for converting liquid air or oxygen into breathable gas |
US3354664A (en) * | 1964-04-11 | 1967-11-28 | Philips Corp | Transferring condensed liquids to a storage container |
US3400758A (en) * | 1966-05-16 | 1968-09-10 | United Aircraft Prod | Helical baffle means in a tubular heat exchanger |
US3552392A (en) | 1968-07-01 | 1971-01-05 | Gen Electric | Aircraft closed circuit breathing system |
US3570481A (en) | 1968-10-23 | 1971-03-16 | Cryogenic Systems Inc | Cryogenic underwater breathing apparatus |
US3572048A (en) * | 1968-10-14 | 1971-03-23 | Wiremold Co | Ominpositional cryogenic underwater breathind apparatus |
US3707078A (en) | 1971-02-10 | 1972-12-26 | Bendix Corp | Fail-safe liquid oxygen to gaseous oxygen conversion system |
US3710854A (en) * | 1971-02-17 | 1973-01-16 | Gen Electric | Condenser |
US3714942A (en) | 1969-02-03 | 1973-02-06 | Sub Marine Syst Inc | Cryogenic gas processing system |
US3730178A (en) | 1970-03-24 | 1973-05-01 | F Moreland | Deep-sea dive suit and life support system |
US3749155A (en) * | 1970-07-16 | 1973-07-31 | Georges Claude Sa | Exchange process |
US3797262A (en) * | 1972-12-01 | 1974-03-19 | Union Carbide Corp | Cryogenic fluid supply system |
US3807396A (en) | 1967-03-16 | 1974-04-30 | E & M Labor | Life support system and method |
US3831594A (en) | 1973-03-05 | 1974-08-27 | Us Navy | Life support system |
US3837396A (en) * | 1970-09-11 | 1974-09-24 | Borg Warner | Vertical surface vapor condensers |
US3864928A (en) * | 1972-12-01 | 1975-02-11 | Union Carbide Corp | All-attitude cryogenic vapor vent system |
US3898047A (en) | 1973-07-17 | 1975-08-05 | Bendix Corp | Oxygen generation system |
US3903962A (en) * | 1974-06-26 | 1975-09-09 | Borg Warner | Condensate guiding apparatus for vertical condensing tubes of vapor condenser |
US3924968A (en) | 1972-07-27 | 1975-12-09 | Gen Motors Corp | Radial compressor with muffled gas chambers and short stable piston skirts and method of assembling same |
US3935715A (en) * | 1974-06-26 | 1976-02-03 | Borg-Warner Corporation | Vapor condenser for a refrigeration system |
US3964866A (en) | 1974-09-13 | 1976-06-22 | William Barney Shelby | Helium reclamation |
US3983861A (en) * | 1975-08-21 | 1976-10-05 | Westman Manufacturing Company | Solar energy conversion device |
US4013429A (en) | 1975-06-04 | 1977-03-22 | Air Products And Chemicals, Inc. | Fractionation of air by adsorption |
US4017284A (en) | 1973-05-14 | 1977-04-12 | Cryox Corporation | Air distillation apparatus comprising regenerator means for producing oxygen |
US4098303A (en) * | 1976-09-17 | 1978-07-04 | Robert Brown Associates | Vapor recovery system for loading backs and storage tanks |
US4181126A (en) | 1978-01-23 | 1980-01-01 | Hendry Stephen M | Cryogenic, underwater-breathing apparatus |
US4194890A (en) | 1976-11-26 | 1980-03-25 | Greene & Kellogg, Inc. | Pressure swing adsorption process and system for gas separation |
US4194891A (en) * | 1978-12-27 | 1980-03-25 | Union Carbide Corporation | Multiple bed rapid pressure swing adsorption for oxygen |
US4198213A (en) | 1978-01-26 | 1980-04-15 | The Garrett Corporation | Self adjusting oxygen enrichment system |
US4211086A (en) * | 1977-10-11 | 1980-07-08 | Beatrice Foods Company | Cryogenic breathing system |
US4222750A (en) | 1976-08-16 | 1980-09-16 | Champion Spark Plug Company | Oxygen enrichment system for medical use |
US4253519A (en) * | 1979-06-22 | 1981-03-03 | Union Carbide Corporation | Enhancement for film condensation apparatus |
US4263018A (en) | 1978-02-01 | 1981-04-21 | Greene & Kellogg | Pressure swing adsorption process and system for gas separation |
US4279127A (en) | 1979-03-02 | 1981-07-21 | Air Products And Chemicals, Inc. | Removable refrigerator for maintaining liquefied gas inventory |
US4331455A (en) | 1979-05-11 | 1982-05-25 | Osaka Oxygen Industries, Ltd. | Method of producing oxygen rich gas utilizing an oxygen concentrator having good start-up characteristics |
US4349357A (en) | 1980-06-23 | 1982-09-14 | Stanley Aviation Corporation | Apparatus and method for fractionating air and other gaseous mixtures |
US4360059A (en) * | 1977-10-01 | 1982-11-23 | Funke Warmeaustauscher Apparatebau Kg | Tube type heat exchanger |
US4404005A (en) * | 1980-08-18 | 1983-09-13 | Normalair-Garrett (Holdings) Limited | Molecular sieve type gas separation systems |
US4428372A (en) | 1980-07-31 | 1984-01-31 | Linde Aktiengesellschaft | Process and apparatus for providing breathing gas |
US4449990A (en) | 1982-09-10 | 1984-05-22 | Invacare Respiratory Corp. | Method and apparatus for fractioning oxygen |
US4465436A (en) | 1981-05-25 | 1984-08-14 | Siemens Aktiengesellschaft | Radial piston compressor |
US4493368A (en) * | 1981-06-22 | 1985-01-15 | Norsk Hydro A.S. | Helical flow heat exchanger having individually adjustable baffles |
US4510760A (en) | 1984-03-02 | 1985-04-16 | Messer Griesheim Industries, Inc. | Compact integrated gas phase separator and subcooler and process |
US4513587A (en) * | 1981-09-14 | 1985-04-30 | Sueddeutsche Kuehlerfabrik Julius Fr. Behr Gmbh & Co., Kg | Evaporator particularly suitable for air conditioners in automotive vehicles |
US4516424A (en) | 1982-07-09 | 1985-05-14 | Hudson Oxygen Therapy Sales Company | Oxygen concentrator monitor and regulation assembly |
US4529411A (en) | 1982-03-12 | 1985-07-16 | Standard Oil Company | CO2 Removal from high CO2 content hydrocarbon containing streams |
US4542010A (en) | 1982-06-30 | 1985-09-17 | Bend Research, Inc. | Method and apparatus for producing oxygen and nitrogen and membrane therefor |
US4545790A (en) * | 1983-08-11 | 1985-10-08 | Bio-Care, Incorporated | Oxygen concentrator |
US4552571A (en) | 1984-04-05 | 1985-11-12 | Vbm Corporation | Oxygen generator with two compressor stages |
US4575386A (en) | 1984-03-29 | 1986-03-11 | U.S. Philips Corporation | Method of liquefying a gas and liquefier for carrying out the method |
US4576616A (en) | 1982-07-27 | 1986-03-18 | Proto-Med. Inc. | Method and apparatus for concentrating oxygen |
US4583364A (en) | 1985-08-19 | 1986-04-22 | Sunpower, Inc. | Piston centering method and apparatus for free-piston Stirling engines |
US4587967A (en) | 1985-07-09 | 1986-05-13 | Lifecare Services, Inc. | Oxygen enriched reciprocating piston respirator |
US4591365A (en) | 1983-10-15 | 1986-05-27 | Linde Aktiengesellschaft | Semipermeable membrane gas separation system |
US4602174A (en) | 1983-12-01 | 1986-07-22 | Sunpower, Inc. | Electromechanical transducer particularly suitable for a linear alternator driven by a free-piston stirling engine |
US4610700A (en) | 1983-11-04 | 1986-09-09 | Union Carbide Corporation | Adsorbent composition useful in retarding corrosion in mufflers |
US4627860A (en) | 1982-07-09 | 1986-12-09 | Hudson Oxygen Therapy Sales Company | Oxygen concentrator and test apparatus |
US4636226A (en) | 1985-08-26 | 1987-01-13 | Vbm Corporation | High pressure oxygen production system |
US4640031A (en) | 1982-11-12 | 1987-02-03 | N.V. W.A. Hoek's Machine | Gas cylinder identification device |
US4670223A (en) | 1983-01-26 | 1987-06-02 | Le Masne S.A. | Apparatus for producing sterile air for medical use |
US4673415A (en) | 1986-05-22 | 1987-06-16 | Vbm Corporation | Oxygen production system with two stage oxygen pressurization |
US4698075A (en) | 1986-06-05 | 1987-10-06 | International Oxygen Company, Inc. | Control system for fluid absorption systems and the like |
US4701187A (en) | 1986-11-03 | 1987-10-20 | Air Products And Chemicals, Inc. | Process for separating components of a gas stream |
US4704146A (en) * | 1986-07-31 | 1987-11-03 | Kryos Energy Inc. | Liquid carbon dioxide recovery from gas mixtures with methane |
US4706664A (en) | 1986-04-11 | 1987-11-17 | Puritan-Bennett Corporation | Inspiration oxygen saver |
EP0247365A2 (en) | 1986-05-30 | 1987-12-02 | Körber Ag | Filling apparatus for oxygen bottles for use in the medicinal oxygen therapy |
US4717406A (en) | 1986-07-07 | 1988-01-05 | Liquid Air Corporation | Cryogenic liquified gas purification method and apparatus |
US4765804A (en) | 1986-10-01 | 1988-08-23 | The Boc Group, Inc. | PSA process and apparatus employing gaseous diffusion barriers |
US4822394A (en) * | 1987-09-14 | 1989-04-18 | Vertech Treatment Systems, Inc. | Method and apparatus for the production and liquefaction of gases |
US4826510A (en) | 1988-01-13 | 1989-05-02 | The John Bunn Company | Portable low profile DC oxygen concentrator |
US4827643A (en) | 1984-12-31 | 1989-05-09 | Aga Gas Central, Inc. | Identification device for a container |
US4841732A (en) | 1987-12-28 | 1989-06-27 | Sarcia Domenico S | System and apparatus for producing and storing liquid gases |
US4844059A (en) | 1986-01-22 | 1989-07-04 | Draegerwerk Ag | Method and apparatus for enriching respiratory gas with oxygen and delivering it to a patient |
US4848447A (en) * | 1983-07-06 | 1989-07-18 | Sladky Hans | Tube-type heat exchanger and liquid distributor head therefor |
US4850426A (en) * | 1987-10-29 | 1989-07-25 | Vicarb | Gas/liquid heat exchanger with condensation |
US4867766A (en) | 1988-09-12 | 1989-09-19 | Union Carbide Corporation | Oxygen enriched air system |
US4869733A (en) | 1986-05-22 | 1989-09-26 | Vbm Corporation | Super-enriched oxygen generator |
US4870960A (en) | 1985-10-07 | 1989-10-03 | Litton Systems, Inc. | Backup breathing gas supply for an oxygen concentrator system |
US4880443A (en) * | 1988-12-22 | 1989-11-14 | The United States Of America As Represented By The Secretary Of The Air Force | Molecular sieve oxygen concentrator with secondary oxygen purifier |
US4899810A (en) * | 1987-10-22 | 1990-02-13 | General Electric Company | Low pressure drop condenser/heat pipe heat exchanger |
US4905685A (en) | 1987-04-14 | 1990-03-06 | Siemens Aktiengesellschaft | Inhalation anaesthesia equipment |
US4922900A (en) | 1988-05-19 | 1990-05-08 | Dragerwerk Aktiengesellschaft | Pumping arrangement for supplying a ventilating apparatus with breathing gas |
US4948391A (en) | 1988-05-12 | 1990-08-14 | Vacuum Optics Corporation Of Japan | Pressure swing adsorption process for gas separation |
US4957107A (en) | 1988-05-10 | 1990-09-18 | Sipin Anatole J | Gas delivery means |
US4971609A (en) | 1990-02-05 | 1990-11-20 | Pawlos Robert A | Portable oxygen concentrator |
US4979882A (en) | 1989-03-13 | 1990-12-25 | Wisconsin Alumni Research Foundation | Spherical rotary machine having six rotary pistons |
US4983190A (en) | 1985-05-21 | 1991-01-08 | Pall Corporation | Pressure-swing adsorption system and method for NBC collective protection |
US4991616A (en) | 1988-01-11 | 1991-02-12 | Desarrollos, Estudios Y Patentes, S.A. | Installation for the supply of oxygen in hospitals and the like |
US5002591A (en) * | 1988-10-14 | 1991-03-26 | Vbm Corporation | High efficiency PSA gas concentrator |
US5048600A (en) * | 1990-10-10 | 1991-09-17 | T & G Technologies, Inc. | Condensor using both film-wise and drop-wise condensation |
US5060480A (en) | 1990-10-30 | 1991-10-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the liquefaction of a flow of gaseous oxygen |
US5071453A (en) | 1989-09-28 | 1991-12-10 | Litton Systems, Inc. | Oxygen concentrator with pressure booster and oxygen concentration monitoring |
US5076823A (en) | 1990-03-20 | 1991-12-31 | Air Products And Chemicals, Inc. | Process for cryogenic air separation |
US5078757A (en) | 1989-05-24 | 1992-01-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for the production of gaseous oxygen under pressure |
US5144945A (en) | 1989-04-20 | 1992-09-08 | Nippon Sanso Kabushiki Kaisha | Portable oxygen-enriching air inhaler |
US5154737A (en) | 1990-01-12 | 1992-10-13 | Vbm Corporation | System for eliminating air leakage and high purity oxygen of a PSA oxygen concentrator |
US5158584A (en) | 1987-10-23 | 1992-10-27 | Teijin Limited | Oxygen enriching module and oxygen enriching apparatus using same |
US5163297A (en) | 1991-01-15 | 1992-11-17 | Iwatani International Corporation | Device for preventing evaporation of liquefied gas in a liquefied gas reservoir |
US5163978A (en) | 1991-10-08 | 1992-11-17 | Praxair Technology, Inc. | Dual product pressure swing adsorption process and system |
US5195874A (en) | 1990-06-19 | 1993-03-23 | Tokico Ltd. | Multistage compressor |
US5199423A (en) | 1990-02-10 | 1993-04-06 | Normalair-Garrett (Holdings) Ltd. | Oxygen-rich gas breathing systems for passenger carrying aircraft |
US5207806A (en) | 1991-10-08 | 1993-05-04 | Praxair Technology, Inc. | Dual product pressure swing adsorption and membrane operations |
US5231835A (en) * | 1992-06-05 | 1993-08-03 | Praxair Technology, Inc. | Liquefier process |
US5237987A (en) | 1990-06-07 | 1993-08-24 | Infrasonics, Inc. | Human lung ventilator system |
US5248320A (en) | 1991-11-11 | 1993-09-28 | The Boc Group Plc | Compressing oxygen |
US5271231A (en) * | 1992-08-10 | 1993-12-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for gas liquefaction with plural work expansion of feed as refrigerant and air separation cycle embodying the same |
US5342176A (en) | 1993-04-05 | 1994-08-30 | Sunpower, Inc. | Method and apparatus for measuring piston position in a free piston compressor |
US5354361A (en) | 1993-05-28 | 1994-10-11 | Litton Industries, Inc. | Energy recovering pressure balance scheme for a combination pressure swing absorber with a boost compressor |
US5388413A (en) | 1993-01-22 | 1995-02-14 | Major; Thomas O. | Portable nitrogen source |
US5405249A (en) | 1992-11-11 | 1995-04-11 | Ultra Electronics Limited | Gas supply apparatus |
US5454429A (en) * | 1992-05-23 | 1995-10-03 | Neurauter; Peter | Rods and mandrel turbulators for heat exchanger |
US5458190A (en) * | 1986-07-29 | 1995-10-17 | Showa Aluminum Corporation | Condenser |
US5461859A (en) | 1994-09-08 | 1995-10-31 | Sunpower, Inc. | Centering system with one way valve for free piston machine |
US5474595A (en) | 1994-04-25 | 1995-12-12 | Airsep Corporation | Capacity control system for pressure swing adsorption apparatus and associated method |
US5477689A (en) * | 1993-09-01 | 1995-12-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure |
US5490871A (en) | 1993-01-30 | 1996-02-13 | The Boc Group Plc | Gas separation |
US5499623A (en) | 1992-02-22 | 1996-03-19 | Dragerwerk Ag | Gas mask and breathing equipment with liquefied respiration gas |
US5525845A (en) | 1994-03-21 | 1996-06-11 | Sunpower, Inc. | Fluid bearing with compliant linkage for centering reciprocating bodies |
US5531807A (en) * | 1994-11-30 | 1996-07-02 | Airsep Corporation | Apparatus and method for supplying oxygen to passengers on board aircraft |
US5539188A (en) | 1991-12-20 | 1996-07-23 | Gemplus Card International | System for the identification of containers, notably gas cylinders |
US5555655A (en) | 1994-09-26 | 1996-09-17 | Aga Ab | Identification device for a container |
US5558139A (en) | 1995-02-13 | 1996-09-24 | Essex Cryogenics Of Missouri | Liquid oxygen system |
US5558086A (en) | 1992-12-16 | 1996-09-24 | Freedom Air Services | Method and apparatus for the intermittent delivery of oxygen therapy to a person |
US5572880A (en) | 1995-04-21 | 1996-11-12 | Figgie International Inc. | Apparatus for providing a conditioned airflow inside a microenvironment and method |
US5584669A (en) | 1993-04-15 | 1996-12-17 | Knf Neuberger Gmbh | Two-stage positive displacement pump |
US5584194A (en) | 1995-10-31 | 1996-12-17 | Gardner; Thomas W. | Method and apparatus for producing liquid nitrogen |
US5593478A (en) | 1994-09-28 | 1997-01-14 | Sequal Technologies, Inc. | Fluid fractionator |
US5593291A (en) | 1995-07-25 | 1997-01-14 | Thomas Industries Inc. | Fluid pumping apparatus |
US5634517A (en) * | 1994-01-27 | 1997-06-03 | Siemens-Elema Ab | Device for reducing the relative humidity of a flowing gas |
US5678536A (en) | 1995-09-05 | 1997-10-21 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Liquid air mixing system |
US5697228A (en) * | 1995-11-17 | 1997-12-16 | The Boc Group Plc | Gas manufacture |
US5704964A (en) | 1994-12-27 | 1998-01-06 | Nippon Sanso Corporation | Pressure swing adsorption process |
US5709203A (en) | 1992-05-07 | 1998-01-20 | Aerospace Design And Development, Inc. | Self contained, cryogenic mixed gas single phase storage and delivery system and method for body cooling, gas conditioning and utilization |
US5726908A (en) | 1995-03-20 | 1998-03-10 | Figgie International Inc. | Liquid quantity sensor and method |
US5823186A (en) | 1996-06-20 | 1998-10-20 | Dragerwerk Ag | Respirator |
US5827358A (en) * | 1996-11-08 | 1998-10-27 | Impact Mst, Incorporation | Rapid cycle pressure swing adsorption oxygen concentration method and apparatus |
US5858062A (en) | 1997-02-10 | 1999-01-12 | Litton Systems, Inc. | Oxygen concentrator |
US5875783A (en) | 1997-04-09 | 1999-03-02 | Dragerwerk Ag | Gas delivery means for respirators and anesthesia apparatus |
US5893944A (en) | 1997-09-30 | 1999-04-13 | Dong; Jung Hyi | Portable PSA oxygen generator |
US5893275A (en) * | 1997-09-04 | 1999-04-13 | In-X Corporation | Compact small volume liquid oxygen production system |
US5901758A (en) | 1997-04-30 | 1999-05-11 | The Boc Group, Inc. | Method of filling gas containers |
US5979440A (en) | 1997-06-16 | 1999-11-09 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US5979182A (en) | 1997-03-13 | 1999-11-09 | Kabushiki Kaisha Kobe Seiko Sho | Method of and apparatus for air separation |
US5988165A (en) | 1997-10-01 | 1999-11-23 | Invacare Corporation | Apparatus and method for forming oxygen-enriched gas and compression thereof for high-pressure mobile storage utilization |
US6004378A (en) | 1991-03-01 | 1999-12-21 | Bayer Aktiengesellschaft | Oxygen enrichment process |
US6012453A (en) | 1995-04-20 | 2000-01-11 | Figgie Inernational Inc. | Apparatus for withdrawal of liquid from a container and method |
US6029473A (en) * | 1997-10-06 | 2000-02-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for filling a reservoir under pressure |
US6035894A (en) | 1996-07-30 | 2000-03-14 | Weh Gmbh Verbindungstechnik | Coupling device for rapid connection |
US6079459A (en) | 1998-02-11 | 2000-06-27 | Welding Company Of America | Controller for tank-filling system |
US6089226A (en) | 1996-11-22 | 2000-07-18 | Aerospace Design & Development, Inc. | Self contained, cryogenic mixed gas single phase storage and delivery |
US6132177A (en) | 1997-08-14 | 2000-10-17 | Bristol Compressors, Inc. | Two stage reciprocating compressors and associated HVAC systems and methods |
US6212904B1 (en) | 1999-11-01 | 2001-04-10 | In-X Corporation | Liquid oxygen production |
US6230516B1 (en) | 2000-02-04 | 2001-05-15 | Andonian Family Nominee Trust | Apparatus for mixing a multiple constituent liquid into a container and method |
US6230518B1 (en) | 1998-09-23 | 2001-05-15 | Linde Aktiengesellschaft | Process and liquefier for the production of liquid air |
US6289981B1 (en) * | 1997-05-30 | 2001-09-18 | Showa Denko K.K. | Multi-bored flat tube for use in a heat exchanger and heat exchanger including said tubes |
US6314957B1 (en) | 1999-04-13 | 2001-11-13 | Air Liquide Sante (International) | Portable home oxygen therapy medical equipment |
US6342090B1 (en) | 2000-05-16 | 2002-01-29 | Litton Systems, Inc. | Gas generating system with multi-rate charging feature |
US6393802B1 (en) | 1999-12-22 | 2002-05-28 | Sunrise Medical Hhg, Inc. | Cylinder filler for use with an oxygen concentrator |
US6422237B1 (en) | 1999-05-18 | 2002-07-23 | DRäGER MEDIZINTECHNIK GMBH | Respirator with a breathing circuit |
US6446630B1 (en) | 1999-02-11 | 2002-09-10 | Sunrise Medical Hhg Inc | Cylinder filling medical oxygen concentrator |
US6520176B1 (en) | 2000-05-25 | 2003-02-18 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Portable oxygen concentrator |
US6530421B1 (en) * | 1997-12-16 | 2003-03-11 | York International Corporation | Counterflow evaporator for refrigerants |
US6651658B1 (en) | 2000-08-03 | 2003-11-25 | Sequal Technologies, Inc. | Portable oxygen concentration system and method of using the same |
US6719019B2 (en) | 2002-06-28 | 2004-04-13 | Litton Systems, Inc. | Deployable oxygen charging system |
US20050072423A1 (en) | 2003-10-07 | 2005-04-07 | Deane Geoffrey Frank | Portable gas fractionalization system |
US6889726B2 (en) | 2002-10-25 | 2005-05-10 | Invacare Corporation | Method and apparatus for filling portable high pressure cylinders with respiratory oxygen |
US6904913B2 (en) | 2002-10-24 | 2005-06-14 | Acoba, Llc | Method and system for delivery of therapeutic gas to a patient and for filling a cylinder |
US20050136299A1 (en) | 2003-12-17 | 2005-06-23 | Richey Joseph B.Ii | Oxygen supply system |
US20050274142A1 (en) | 2004-06-14 | 2005-12-15 | Corey John A | Cryogenically producing oxygen-enriched liquid and/or gaseous oxygen from atmospheric air |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US35099A (en) * | 1862-04-29 | Improvement in machines for boring seats of buggies | ||
GB1185199A (en) * | 1967-04-06 | 1970-03-25 | Firewell Company Inc | Breathing pack for converting liquid air or oxygen into breathing gas |
GB1336892A (en) * | 1971-05-17 | 1973-11-14 | Nii Kriogennoi Elektroniki | Refrigerant for a cryogenic throttling unit |
GB1416163A (en) * | 1972-01-07 | 1975-12-03 | Boc International Ltd | Air separation |
US4697635A (en) * | 1984-07-05 | 1987-10-06 | Apd Cryogenics Inc. | Parallel wrapped tube heat exchanger |
JPH0621006B2 (en) * | 1985-12-23 | 1994-03-23 | 日本酸素株式会社 | High-concentration oxygen gas production equipment by pressure fluctuation adsorption method |
US4785879A (en) * | 1986-01-14 | 1988-11-22 | Apd Cryogenics | Parallel wrapped tube heat exchanger |
US4802899A (en) * | 1987-09-21 | 1989-02-07 | Airsep Corporation | Pressure swing adsorption apparatus |
US5268021A (en) * | 1989-11-20 | 1993-12-07 | Dynotec Corporation | Fluid fractionator |
US5112367A (en) * | 1989-11-20 | 1992-05-12 | Hill Charles C | Fluid fractionator |
US5361591A (en) * | 1992-04-15 | 1994-11-08 | Oceaneering International, Inc. | Portable life support system |
JPH0726784B2 (en) * | 1992-09-25 | 1995-03-29 | 岩谷産業株式会社 | Simple liquid nitrogen production equipment |
US5337572A (en) * | 1993-05-04 | 1994-08-16 | Apd Cryogenics, Inc. | Cryogenic refrigerator with single stage compressor |
US5441658A (en) * | 1993-11-09 | 1995-08-15 | Apd Cryogenics, Inc. | Cryogenic mixed gas refrigerant for operation within temperature ranges of 80°K- 100°K |
US5519999A (en) * | 1994-08-05 | 1996-05-28 | Trw Inc. | Flow turning cryogenic heat exchanger |
US5579654A (en) * | 1995-06-29 | 1996-12-03 | Apd Cryogenics, Inc. | Cryostat refrigeration system using mixed refrigerants in a closed vapor compression cycle having a fixed flow restrictor |
US5595065A (en) * | 1995-07-07 | 1997-01-21 | Apd Cryogenics | Closed cycle cryogenic refrigeration system with automatic variable flow area throttling device |
-
1997
- 1997-06-16 US US08/876,970 patent/US5979440A/en not_active Expired - Lifetime
-
1998
- 1998-06-03 WO PCT/US1998/011154 patent/WO1998058219A1/en active IP Right Grant
- 1998-06-03 JP JP50445499A patent/JP4183760B2/en not_active Expired - Lifetime
- 1998-06-03 DE DE69800669T patent/DE69800669T2/en not_active Expired - Lifetime
- 1998-06-03 EP EP98926158A patent/EP0990107B1/en not_active Expired - Lifetime
- 1998-06-03 AT AT98926158T patent/ATE200349T1/en not_active IP Right Cessation
- 1998-06-03 CA CA002293287A patent/CA2293287C/en not_active Expired - Lifetime
-
1999
- 1999-06-29 US US09/343,149 patent/US6681764B1/en not_active Expired - Lifetime
- 1999-06-29 US US09/342,890 patent/US6651653B1/en not_active Expired - Lifetime
- 1999-10-19 US US09/420,892 patent/US6698423B1/en not_active Ceased
-
2006
- 2006-03-01 US US11/366,986 patent/USRE43398E1/en not_active Expired - Lifetime
-
2008
- 2008-04-11 JP JP2008103219A patent/JP4729593B2/en not_active Expired - Lifetime
Patent Citations (227)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US621536A (en) * | 1899-03-21 | Apparatus for liquefying air | ||
US621537A (en) * | 1899-03-21 | Apparatus for liquefying gas | ||
US948835A (en) * | 1910-02-08 | Bruce Walter | Ammonia-condenser. | |
US609499A (en) * | 1898-08-23 | chatwood | ||
US665912A (en) * | 1900-01-03 | 1901-01-15 | Emile Jolicard | Boiler. |
US707633A (en) * | 1901-02-15 | 1902-08-26 | James F Place | Art or process of liquefying air or other gases and cooling by means thereof. |
US718572A (en) * | 1902-02-17 | 1903-01-13 | Edwin Joseph Richardson | Apparatus for the liquefaction of air or other aeriform fluids. |
US879302A (en) * | 1905-04-03 | 1908-02-18 | Colorado Iron Works Co | Blast-heating apparatus. |
US881176A (en) * | 1906-02-23 | 1908-03-10 | Georges Claude | Apparatus for the liquefaction of air. |
US1454053A (en) * | 1920-02-18 | 1923-05-08 | Griscom Russell Co | Oil cooler |
US1867163A (en) * | 1925-01-26 | 1932-07-12 | Louis Chavanne J | Heat recuperation |
USRE19031E (en) | 1926-12-29 | 1933-12-19 | Process and apparatus for the | |
US1957006A (en) * | 1927-04-27 | 1934-05-01 | Sulphide Corp | Method of and apparatus for condensing sulphur |
US1782409A (en) * | 1927-12-19 | 1930-11-25 | Griscom Russell Co | Heat exchanger |
US1796510A (en) * | 1929-06-17 | 1931-03-17 | Delas Francois Xavier J Albert | Surface condenser and the like |
US1821080A (en) * | 1930-10-15 | 1931-09-01 | Engineering Products Corp Inc | Radiator |
US2017676A (en) * | 1933-03-11 | 1935-10-15 | American Lurgi Corp | Method of and apparatus for condensing sulphuric acid |
US2194654A (en) * | 1936-05-12 | 1940-03-26 | Hadamovsky Paul | Apparatus for liquefying gases |
US2210031A (en) * | 1936-08-28 | 1940-08-06 | Pfaudler Co Inc | Refrigerating apparatus and method |
US2318206A (en) * | 1940-06-17 | 1943-05-04 | M Werk Company | Apparatus for treating liquids flowing through heated tubes |
US2434519A (en) * | 1942-04-18 | 1948-01-13 | Raskin Walter | Heat exchange conduit with a spiral fin having a capillary groove |
US2384714A (en) * | 1943-04-12 | 1945-09-11 | Tech Studien Ag | Tubular heat exchanger |
US2440245A (en) * | 1944-03-13 | 1948-04-27 | Standard Telephones Cables Ltd | Cooling of high-temperature bodies |
US2751199A (en) * | 1951-04-18 | 1956-06-19 | Taco Heaters Inc | Heat exchanger |
US2797554A (en) * | 1954-01-06 | 1957-07-02 | William J Donovan | Heat exchanger in refrigeration system |
US2960834A (en) * | 1954-11-22 | 1960-11-22 | Garrett Corp | Production of liquid oxygen from atmospheric air |
US2919555A (en) | 1955-07-28 | 1960-01-05 | Joy Mfg Co | Apparatus for and method of separating gases |
US2969957A (en) * | 1956-01-10 | 1961-01-31 | Thomson Houston Comp Francaise | Electric discharge device cooling systems |
US2905447A (en) * | 1956-05-04 | 1959-09-22 | Huet Andre | Tubular heat-exchanger |
US2937079A (en) * | 1956-08-06 | 1960-05-17 | Phillips Petroleum Co | Apparatus for contacting and subsequently separating immiscible liquids |
US3055643A (en) * | 1956-08-06 | 1962-09-25 | Thomson Houston Comp Francaise | Heat exchangers |
US2958204A (en) * | 1956-08-13 | 1960-11-01 | Aro Equipment Corp | Liquid oxygen converter |
US2909903A (en) | 1956-11-07 | 1959-10-27 | Little Inc A | Liquefaction of low-boiling gases |
US2945354A (en) * | 1957-03-18 | 1960-07-19 | North American Aviation Inc | Liquid oxygen conversion system |
US2993682A (en) * | 1957-03-18 | 1961-07-25 | Huet Andre | Heat exchanger tubes |
US2944627A (en) | 1958-02-12 | 1960-07-12 | Exxon Research Engineering Co | Method and apparatus for fractionating gaseous mixtures by adsorption |
US2943454A (en) * | 1958-06-30 | 1960-07-05 | Mine Safety Appliances Co | Liquid oxygen converter |
US2964919A (en) * | 1958-07-07 | 1960-12-20 | British Oxygen Co Ltd | Converter system for liquefied gases |
US3186406A (en) * | 1959-02-21 | 1965-06-01 | Normalair Ltd | Breathing apparatus |
US2970452A (en) * | 1959-04-01 | 1961-02-07 | Union Carbide Corp | Method and apparatus for supplying liquefied gas |
US3152589A (en) * | 1959-04-16 | 1964-10-13 | British Oxygen Co Ltd | Liquid oxygen system for passenger aircraft |
US3097497A (en) | 1959-08-14 | 1963-07-16 | Normalair Ltd | Oxygen supply systems |
US3117426A (en) * | 1960-11-23 | 1964-01-14 | Garrett Corp | Environmental system for protective suit |
US3205670A (en) * | 1962-09-24 | 1965-09-14 | Puritan Compressed Gas Corp | Oxygen supply system |
US3183678A (en) * | 1963-04-29 | 1965-05-18 | Bendix Corp | Liquid to gas conversion system |
US3199303A (en) * | 1963-05-09 | 1965-08-10 | Union Carbide Corp | Oxygen therapy system |
US3313091A (en) | 1963-11-04 | 1967-04-11 | Exxon Research Engineering Co | Vacuum cycle adsorption |
US3354664A (en) * | 1964-04-11 | 1967-11-28 | Philips Corp | Transferring condensed liquids to a storage container |
US3318307A (en) | 1964-08-03 | 1967-05-09 | Firewel Company Inc | Breathing pack for converting liquid air or oxygen into breathable gas |
US3400758A (en) * | 1966-05-16 | 1968-09-10 | United Aircraft Prod | Helical baffle means in a tubular heat exchanger |
US3807396A (en) | 1967-03-16 | 1974-04-30 | E & M Labor | Life support system and method |
US3552392A (en) | 1968-07-01 | 1971-01-05 | Gen Electric | Aircraft closed circuit breathing system |
US3572048A (en) * | 1968-10-14 | 1971-03-23 | Wiremold Co | Ominpositional cryogenic underwater breathind apparatus |
US3570481A (en) | 1968-10-23 | 1971-03-16 | Cryogenic Systems Inc | Cryogenic underwater breathing apparatus |
US3714942A (en) | 1969-02-03 | 1973-02-06 | Sub Marine Syst Inc | Cryogenic gas processing system |
US3730178A (en) | 1970-03-24 | 1973-05-01 | F Moreland | Deep-sea dive suit and life support system |
US3749155A (en) * | 1970-07-16 | 1973-07-31 | Georges Claude Sa | Exchange process |
US3837396A (en) * | 1970-09-11 | 1974-09-24 | Borg Warner | Vertical surface vapor condensers |
US3707078A (en) | 1971-02-10 | 1972-12-26 | Bendix Corp | Fail-safe liquid oxygen to gaseous oxygen conversion system |
US3710854A (en) * | 1971-02-17 | 1973-01-16 | Gen Electric | Condenser |
US3924968A (en) | 1972-07-27 | 1975-12-09 | Gen Motors Corp | Radial compressor with muffled gas chambers and short stable piston skirts and method of assembling same |
US3797262A (en) * | 1972-12-01 | 1974-03-19 | Union Carbide Corp | Cryogenic fluid supply system |
US3864928A (en) * | 1972-12-01 | 1975-02-11 | Union Carbide Corp | All-attitude cryogenic vapor vent system |
US3831594A (en) | 1973-03-05 | 1974-08-27 | Us Navy | Life support system |
US4017284A (en) | 1973-05-14 | 1977-04-12 | Cryox Corporation | Air distillation apparatus comprising regenerator means for producing oxygen |
US3898047A (en) | 1973-07-17 | 1975-08-05 | Bendix Corp | Oxygen generation system |
US3935715A (en) * | 1974-06-26 | 1976-02-03 | Borg-Warner Corporation | Vapor condenser for a refrigeration system |
US3903962A (en) * | 1974-06-26 | 1975-09-09 | Borg Warner | Condensate guiding apparatus for vertical condensing tubes of vapor condenser |
US3964866A (en) | 1974-09-13 | 1976-06-22 | William Barney Shelby | Helium reclamation |
US4013429A (en) | 1975-06-04 | 1977-03-22 | Air Products And Chemicals, Inc. | Fractionation of air by adsorption |
US3983861A (en) * | 1975-08-21 | 1976-10-05 | Westman Manufacturing Company | Solar energy conversion device |
US4222750A (en) | 1976-08-16 | 1980-09-16 | Champion Spark Plug Company | Oxygen enrichment system for medical use |
US4098303A (en) * | 1976-09-17 | 1978-07-04 | Robert Brown Associates | Vapor recovery system for loading backs and storage tanks |
US4194890A (en) | 1976-11-26 | 1980-03-25 | Greene & Kellogg, Inc. | Pressure swing adsorption process and system for gas separation |
US4360059A (en) * | 1977-10-01 | 1982-11-23 | Funke Warmeaustauscher Apparatebau Kg | Tube type heat exchanger |
US4211086A (en) * | 1977-10-11 | 1980-07-08 | Beatrice Foods Company | Cryogenic breathing system |
US4181126A (en) | 1978-01-23 | 1980-01-01 | Hendry Stephen M | Cryogenic, underwater-breathing apparatus |
US4198213A (en) | 1978-01-26 | 1980-04-15 | The Garrett Corporation | Self adjusting oxygen enrichment system |
US4263018A (en) | 1978-02-01 | 1981-04-21 | Greene & Kellogg | Pressure swing adsorption process and system for gas separation |
US4194891A (en) * | 1978-12-27 | 1980-03-25 | Union Carbide Corporation | Multiple bed rapid pressure swing adsorption for oxygen |
US4279127A (en) | 1979-03-02 | 1981-07-21 | Air Products And Chemicals, Inc. | Removable refrigerator for maintaining liquefied gas inventory |
US4331455A (en) | 1979-05-11 | 1982-05-25 | Osaka Oxygen Industries, Ltd. | Method of producing oxygen rich gas utilizing an oxygen concentrator having good start-up characteristics |
US4253519A (en) * | 1979-06-22 | 1981-03-03 | Union Carbide Corporation | Enhancement for film condensation apparatus |
US4349357A (en) | 1980-06-23 | 1982-09-14 | Stanley Aviation Corporation | Apparatus and method for fractionating air and other gaseous mixtures |
US4428372A (en) | 1980-07-31 | 1984-01-31 | Linde Aktiengesellschaft | Process and apparatus for providing breathing gas |
US4404005A (en) * | 1980-08-18 | 1983-09-13 | Normalair-Garrett (Holdings) Limited | Molecular sieve type gas separation systems |
US4465436A (en) | 1981-05-25 | 1984-08-14 | Siemens Aktiengesellschaft | Radial piston compressor |
US4493368A (en) * | 1981-06-22 | 1985-01-15 | Norsk Hydro A.S. | Helical flow heat exchanger having individually adjustable baffles |
US4513587A (en) * | 1981-09-14 | 1985-04-30 | Sueddeutsche Kuehlerfabrik Julius Fr. Behr Gmbh & Co., Kg | Evaporator particularly suitable for air conditioners in automotive vehicles |
US4529411A (en) | 1982-03-12 | 1985-07-16 | Standard Oil Company | CO2 Removal from high CO2 content hydrocarbon containing streams |
US4542010A (en) | 1982-06-30 | 1985-09-17 | Bend Research, Inc. | Method and apparatus for producing oxygen and nitrogen and membrane therefor |
US4516424A (en) | 1982-07-09 | 1985-05-14 | Hudson Oxygen Therapy Sales Company | Oxygen concentrator monitor and regulation assembly |
US4627860A (en) | 1982-07-09 | 1986-12-09 | Hudson Oxygen Therapy Sales Company | Oxygen concentrator and test apparatus |
US4561287A (en) | 1982-07-09 | 1985-12-31 | Hudson Oxygen Therapy Sales Company | Oxygen concentrator |
US4576616A (en) | 1982-07-27 | 1986-03-18 | Proto-Med. Inc. | Method and apparatus for concentrating oxygen |
US4449990A (en) | 1982-09-10 | 1984-05-22 | Invacare Respiratory Corp. | Method and apparatus for fractioning oxygen |
US4640031A (en) | 1982-11-12 | 1987-02-03 | N.V. W.A. Hoek's Machine | Gas cylinder identification device |
US4670223A (en) | 1983-01-26 | 1987-06-02 | Le Masne S.A. | Apparatus for producing sterile air for medical use |
US4848447A (en) * | 1983-07-06 | 1989-07-18 | Sladky Hans | Tube-type heat exchanger and liquid distributor head therefor |
US4545790A (en) * | 1983-08-11 | 1985-10-08 | Bio-Care, Incorporated | Oxygen concentrator |
US4591365A (en) | 1983-10-15 | 1986-05-27 | Linde Aktiengesellschaft | Semipermeable membrane gas separation system |
US4610700A (en) | 1983-11-04 | 1986-09-09 | Union Carbide Corporation | Adsorbent composition useful in retarding corrosion in mufflers |
US4602174A (en) | 1983-12-01 | 1986-07-22 | Sunpower, Inc. | Electromechanical transducer particularly suitable for a linear alternator driven by a free-piston stirling engine |
US4510760A (en) | 1984-03-02 | 1985-04-16 | Messer Griesheim Industries, Inc. | Compact integrated gas phase separator and subcooler and process |
US4575386A (en) | 1984-03-29 | 1986-03-11 | U.S. Philips Corporation | Method of liquefying a gas and liquefier for carrying out the method |
US4552571A (en) | 1984-04-05 | 1985-11-12 | Vbm Corporation | Oxygen generator with two compressor stages |
US4827643A (en) | 1984-12-31 | 1989-05-09 | Aga Gas Central, Inc. | Identification device for a container |
US4983190A (en) | 1985-05-21 | 1991-01-08 | Pall Corporation | Pressure-swing adsorption system and method for NBC collective protection |
US4587967A (en) | 1985-07-09 | 1986-05-13 | Lifecare Services, Inc. | Oxygen enriched reciprocating piston respirator |
US4583364A (en) | 1985-08-19 | 1986-04-22 | Sunpower, Inc. | Piston centering method and apparatus for free-piston Stirling engines |
US4636226A (en) | 1985-08-26 | 1987-01-13 | Vbm Corporation | High pressure oxygen production system |
US4870960A (en) | 1985-10-07 | 1989-10-03 | Litton Systems, Inc. | Backup breathing gas supply for an oxygen concentrator system |
US4844059A (en) | 1986-01-22 | 1989-07-04 | Draegerwerk Ag | Method and apparatus for enriching respiratory gas with oxygen and delivering it to a patient |
US4706664A (en) | 1986-04-11 | 1987-11-17 | Puritan-Bennett Corporation | Inspiration oxygen saver |
US4673415A (en) | 1986-05-22 | 1987-06-16 | Vbm Corporation | Oxygen production system with two stage oxygen pressurization |
US4869733A (en) | 1986-05-22 | 1989-09-26 | Vbm Corporation | Super-enriched oxygen generator |
EP0247365A2 (en) | 1986-05-30 | 1987-12-02 | Körber Ag | Filling apparatus for oxygen bottles for use in the medicinal oxygen therapy |
US4698075A (en) | 1986-06-05 | 1987-10-06 | International Oxygen Company, Inc. | Control system for fluid absorption systems and the like |
US4717406A (en) | 1986-07-07 | 1988-01-05 | Liquid Air Corporation | Cryogenic liquified gas purification method and apparatus |
US5458190A (en) * | 1986-07-29 | 1995-10-17 | Showa Aluminum Corporation | Condenser |
US4704146A (en) * | 1986-07-31 | 1987-11-03 | Kryos Energy Inc. | Liquid carbon dioxide recovery from gas mixtures with methane |
US4765804A (en) | 1986-10-01 | 1988-08-23 | The Boc Group, Inc. | PSA process and apparatus employing gaseous diffusion barriers |
US4701187A (en) | 1986-11-03 | 1987-10-20 | Air Products And Chemicals, Inc. | Process for separating components of a gas stream |
US4905685A (en) | 1987-04-14 | 1990-03-06 | Siemens Aktiengesellschaft | Inhalation anaesthesia equipment |
US4822394A (en) * | 1987-09-14 | 1989-04-18 | Vertech Treatment Systems, Inc. | Method and apparatus for the production and liquefaction of gases |
US4899810A (en) * | 1987-10-22 | 1990-02-13 | General Electric Company | Low pressure drop condenser/heat pipe heat exchanger |
US5158584A (en) | 1987-10-23 | 1992-10-27 | Teijin Limited | Oxygen enriching module and oxygen enriching apparatus using same |
US4850426A (en) * | 1987-10-29 | 1989-07-25 | Vicarb | Gas/liquid heat exchanger with condensation |
US4841732A (en) | 1987-12-28 | 1989-06-27 | Sarcia Domenico S | System and apparatus for producing and storing liquid gases |
US4991616A (en) | 1988-01-11 | 1991-02-12 | Desarrollos, Estudios Y Patentes, S.A. | Installation for the supply of oxygen in hospitals and the like |
US4826510A (en) | 1988-01-13 | 1989-05-02 | The John Bunn Company | Portable low profile DC oxygen concentrator |
US4957107A (en) | 1988-05-10 | 1990-09-18 | Sipin Anatole J | Gas delivery means |
US4948391A (en) | 1988-05-12 | 1990-08-14 | Vacuum Optics Corporation Of Japan | Pressure swing adsorption process for gas separation |
US4922900A (en) | 1988-05-19 | 1990-05-08 | Dragerwerk Aktiengesellschaft | Pumping arrangement for supplying a ventilating apparatus with breathing gas |
US4867766A (en) | 1988-09-12 | 1989-09-19 | Union Carbide Corporation | Oxygen enriched air system |
US5002591A (en) * | 1988-10-14 | 1991-03-26 | Vbm Corporation | High efficiency PSA gas concentrator |
US4880443A (en) * | 1988-12-22 | 1989-11-14 | The United States Of America As Represented By The Secretary Of The Air Force | Molecular sieve oxygen concentrator with secondary oxygen purifier |
US4979882A (en) | 1989-03-13 | 1990-12-25 | Wisconsin Alumni Research Foundation | Spherical rotary machine having six rotary pistons |
US5144945A (en) | 1989-04-20 | 1992-09-08 | Nippon Sanso Kabushiki Kaisha | Portable oxygen-enriching air inhaler |
US5078757A (en) | 1989-05-24 | 1992-01-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for the production of gaseous oxygen under pressure |
US5071453A (en) | 1989-09-28 | 1991-12-10 | Litton Systems, Inc. | Oxygen concentrator with pressure booster and oxygen concentration monitoring |
US5154737A (en) | 1990-01-12 | 1992-10-13 | Vbm Corporation | System for eliminating air leakage and high purity oxygen of a PSA oxygen concentrator |
US4971609A (en) | 1990-02-05 | 1990-11-20 | Pawlos Robert A | Portable oxygen concentrator |
US5199423A (en) | 1990-02-10 | 1993-04-06 | Normalair-Garrett (Holdings) Ltd. | Oxygen-rich gas breathing systems for passenger carrying aircraft |
US5076823A (en) | 1990-03-20 | 1991-12-31 | Air Products And Chemicals, Inc. | Process for cryogenic air separation |
US5237987A (en) | 1990-06-07 | 1993-08-24 | Infrasonics, Inc. | Human lung ventilator system |
US5195874A (en) | 1990-06-19 | 1993-03-23 | Tokico Ltd. | Multistage compressor |
US5048600A (en) * | 1990-10-10 | 1991-09-17 | T & G Technologies, Inc. | Condensor using both film-wise and drop-wise condensation |
US5060480A (en) | 1990-10-30 | 1991-10-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the liquefaction of a flow of gaseous oxygen |
US5163297A (en) | 1991-01-15 | 1992-11-17 | Iwatani International Corporation | Device for preventing evaporation of liquefied gas in a liquefied gas reservoir |
US6004378A (en) | 1991-03-01 | 1999-12-21 | Bayer Aktiengesellschaft | Oxygen enrichment process |
US5163978A (en) | 1991-10-08 | 1992-11-17 | Praxair Technology, Inc. | Dual product pressure swing adsorption process and system |
US5207806A (en) | 1991-10-08 | 1993-05-04 | Praxair Technology, Inc. | Dual product pressure swing adsorption and membrane operations |
US5248320A (en) | 1991-11-11 | 1993-09-28 | The Boc Group Plc | Compressing oxygen |
US5539188A (en) | 1991-12-20 | 1996-07-23 | Gemplus Card International | System for the identification of containers, notably gas cylinders |
US5499623A (en) | 1992-02-22 | 1996-03-19 | Dragerwerk Ag | Gas mask and breathing equipment with liquefied respiration gas |
US6513521B1 (en) | 1992-05-07 | 2003-02-04 | Aerospace Design & Development, Inc. | Cryogenic mixed gas single phase storage and delivery |
US5709203A (en) | 1992-05-07 | 1998-01-20 | Aerospace Design And Development, Inc. | Self contained, cryogenic mixed gas single phase storage and delivery system and method for body cooling, gas conditioning and utilization |
US5454429A (en) * | 1992-05-23 | 1995-10-03 | Neurauter; Peter | Rods and mandrel turbulators for heat exchanger |
US5231835A (en) * | 1992-06-05 | 1993-08-03 | Praxair Technology, Inc. | Liquefier process |
US5271231A (en) * | 1992-08-10 | 1993-12-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for gas liquefaction with plural work expansion of feed as refrigerant and air separation cycle embodying the same |
US5405249A (en) | 1992-11-11 | 1995-04-11 | Ultra Electronics Limited | Gas supply apparatus |
US5558086A (en) | 1992-12-16 | 1996-09-24 | Freedom Air Services | Method and apparatus for the intermittent delivery of oxygen therapy to a person |
US5388413A (en) | 1993-01-22 | 1995-02-14 | Major; Thomas O. | Portable nitrogen source |
US5490871A (en) | 1993-01-30 | 1996-02-13 | The Boc Group Plc | Gas separation |
US5342176A (en) | 1993-04-05 | 1994-08-30 | Sunpower, Inc. | Method and apparatus for measuring piston position in a free piston compressor |
US5496153A (en) | 1993-04-05 | 1996-03-05 | Sunpower, Inc. | Method and apparatus for measuring piston position in a free piston compressor |
US5584669A (en) | 1993-04-15 | 1996-12-17 | Knf Neuberger Gmbh | Two-stage positive displacement pump |
US5354361A (en) | 1993-05-28 | 1994-10-11 | Litton Industries, Inc. | Energy recovering pressure balance scheme for a combination pressure swing absorber with a boost compressor |
US5477689A (en) * | 1993-09-01 | 1995-12-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure |
US5634517A (en) * | 1994-01-27 | 1997-06-03 | Siemens-Elema Ab | Device for reducing the relative humidity of a flowing gas |
US5525845A (en) | 1994-03-21 | 1996-06-11 | Sunpower, Inc. | Fluid bearing with compliant linkage for centering reciprocating bodies |
US5474595A (en) | 1994-04-25 | 1995-12-12 | Airsep Corporation | Capacity control system for pressure swing adsorption apparatus and associated method |
US5461859A (en) | 1994-09-08 | 1995-10-31 | Sunpower, Inc. | Centering system with one way valve for free piston machine |
US5555655A (en) | 1994-09-26 | 1996-09-17 | Aga Ab | Identification device for a container |
US5593478A (en) | 1994-09-28 | 1997-01-14 | Sequal Technologies, Inc. | Fluid fractionator |
US5730778A (en) | 1994-09-28 | 1998-03-24 | Sequal Technologies, Inc. | Fluid fractionator |
US5531807A (en) * | 1994-11-30 | 1996-07-02 | Airsep Corporation | Apparatus and method for supplying oxygen to passengers on board aircraft |
US5704964A (en) | 1994-12-27 | 1998-01-06 | Nippon Sanso Corporation | Pressure swing adsorption process |
US5558139A (en) | 1995-02-13 | 1996-09-24 | Essex Cryogenics Of Missouri | Liquid oxygen system |
US5726908A (en) | 1995-03-20 | 1998-03-10 | Figgie International Inc. | Liquid quantity sensor and method |
US6012453A (en) | 1995-04-20 | 2000-01-11 | Figgie Inernational Inc. | Apparatus for withdrawal of liquid from a container and method |
US5572880A (en) | 1995-04-21 | 1996-11-12 | Figgie International Inc. | Apparatus for providing a conditioned airflow inside a microenvironment and method |
US5689968A (en) | 1995-04-21 | 1997-11-25 | Figgie International Inc. | Apparatus for providing a conditioned airflow inside a microenvironment and method |
US5593291A (en) | 1995-07-25 | 1997-01-14 | Thomas Industries Inc. | Fluid pumping apparatus |
US5678536A (en) | 1995-09-05 | 1997-10-21 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Liquid air mixing system |
US5584194A (en) | 1995-10-31 | 1996-12-17 | Gardner; Thomas W. | Method and apparatus for producing liquid nitrogen |
US5697228A (en) * | 1995-11-17 | 1997-12-16 | The Boc Group Plc | Gas manufacture |
US5823186A (en) | 1996-06-20 | 1998-10-20 | Dragerwerk Ag | Respirator |
US6035894A (en) | 1996-07-30 | 2000-03-14 | Weh Gmbh Verbindungstechnik | Coupling device for rapid connection |
US5827358A (en) * | 1996-11-08 | 1998-10-27 | Impact Mst, Incorporation | Rapid cycle pressure swing adsorption oxygen concentration method and apparatus |
US6089226A (en) | 1996-11-22 | 2000-07-18 | Aerospace Design & Development, Inc. | Self contained, cryogenic mixed gas single phase storage and delivery |
US5858062A (en) | 1997-02-10 | 1999-01-12 | Litton Systems, Inc. | Oxygen concentrator |
US5979182A (en) | 1997-03-13 | 1999-11-09 | Kabushiki Kaisha Kobe Seiko Sho | Method of and apparatus for air separation |
US5875783A (en) | 1997-04-09 | 1999-03-02 | Dragerwerk Ag | Gas delivery means for respirators and anesthesia apparatus |
US5901758A (en) | 1997-04-30 | 1999-05-11 | The Boc Group, Inc. | Method of filling gas containers |
US6289981B1 (en) * | 1997-05-30 | 2001-09-18 | Showa Denko K.K. | Multi-bored flat tube for use in a heat exchanger and heat exchanger including said tubes |
US6681764B1 (en) * | 1997-06-16 | 2004-01-27 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US5979440A (en) | 1997-06-16 | 1999-11-09 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
US6132177A (en) | 1997-08-14 | 2000-10-17 | Bristol Compressors, Inc. | Two stage reciprocating compressors and associated HVAC systems and methods |
US5893275A (en) * | 1997-09-04 | 1999-04-13 | In-X Corporation | Compact small volume liquid oxygen production system |
US5893944A (en) | 1997-09-30 | 1999-04-13 | Dong; Jung Hyi | Portable PSA oxygen generator |
US5988165A (en) | 1997-10-01 | 1999-11-23 | Invacare Corporation | Apparatus and method for forming oxygen-enriched gas and compression thereof for high-pressure mobile storage utilization |
US20060000474A1 (en) | 1997-10-01 | 2006-01-05 | Richey Joseph B Ii | Oxygen conserving device utilizing a radial multi-stage compressor for high-pressure mobile storage |
US6805122B2 (en) | 1997-10-01 | 2004-10-19 | Invacare Corporation | Oxygen conserving device utilizing a radial multi-stage compressor for high-pressure mobile storage |
US6302107B1 (en) | 1997-10-01 | 2001-10-16 | Invacare Corporation | Apparatus and method for forming oxygen-enriched gas and compression thereof for high-pressure mobile storage utilization |
US6923180B2 (en) | 1997-10-01 | 2005-08-02 | Invacare Corporation | Oxygen conserving device utilizing a radial multi-stage compressor for high-pressure mobile storage |
US6029473A (en) * | 1997-10-06 | 2000-02-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for filling a reservoir under pressure |
US6530421B1 (en) * | 1997-12-16 | 2003-03-11 | York International Corporation | Counterflow evaporator for refrigerants |
US6079459A (en) | 1998-02-11 | 2000-06-27 | Welding Company Of America | Controller for tank-filling system |
US6230518B1 (en) | 1998-09-23 | 2001-05-15 | Linde Aktiengesellschaft | Process and liquefier for the production of liquid air |
US6446630B1 (en) | 1999-02-11 | 2002-09-10 | Sunrise Medical Hhg Inc | Cylinder filling medical oxygen concentrator |
US6314957B1 (en) | 1999-04-13 | 2001-11-13 | Air Liquide Sante (International) | Portable home oxygen therapy medical equipment |
US6422237B1 (en) | 1999-05-18 | 2002-07-23 | DRäGER MEDIZINTECHNIK GMBH | Respirator with a breathing circuit |
US6212904B1 (en) | 1999-11-01 | 2001-04-10 | In-X Corporation | Liquid oxygen production |
US6393802B1 (en) | 1999-12-22 | 2002-05-28 | Sunrise Medical Hhg, Inc. | Cylinder filler for use with an oxygen concentrator |
US6230516B1 (en) | 2000-02-04 | 2001-05-15 | Andonian Family Nominee Trust | Apparatus for mixing a multiple constituent liquid into a container and method |
US6342090B1 (en) | 2000-05-16 | 2002-01-29 | Litton Systems, Inc. | Gas generating system with multi-rate charging feature |
US6520176B1 (en) | 2000-05-25 | 2003-02-18 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Portable oxygen concentrator |
US6651658B1 (en) | 2000-08-03 | 2003-11-25 | Sequal Technologies, Inc. | Portable oxygen concentration system and method of using the same |
US6719019B2 (en) | 2002-06-28 | 2004-04-13 | Litton Systems, Inc. | Deployable oxygen charging system |
US6904913B2 (en) | 2002-10-24 | 2005-06-14 | Acoba, Llc | Method and system for delivery of therapeutic gas to a patient and for filling a cylinder |
US6889726B2 (en) | 2002-10-25 | 2005-05-10 | Invacare Corporation | Method and apparatus for filling portable high pressure cylinders with respiratory oxygen |
US20050115630A1 (en) | 2002-10-25 | 2005-06-02 | Richey Joseph B.Ii | Method and apparatus for filling portable high pressure cylinders with respiratory oxygen |
US20050072423A1 (en) | 2003-10-07 | 2005-04-07 | Deane Geoffrey Frank | Portable gas fractionalization system |
US20050136299A1 (en) | 2003-12-17 | 2005-06-23 | Richey Joseph B.Ii | Oxygen supply system |
US20050274142A1 (en) | 2004-06-14 | 2005-12-15 | Corey John A | Cryogenically producing oxygen-enriched liquid and/or gaseous oxygen from atmospheric air |
Non-Patent Citations (3)
Title |
---|
"Design Manual for Two-Phase Components of Spacecraft Thermal Management Systems"; PL-TR-92-3002, Crowley et al, Phillips Laboratory, Sep. 1992. |
"Hautkondensation an feingewelten Oberflachen bei Beruckischtigun der Obrflachenspannungen"; Von Romano Gregoric, vol. V, 1954 (in German). |
USPTO Reexam Control No. 90/008,167. |
Cited By (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9421338B2 (en) | 2008-03-31 | 2016-08-23 | Covidien Lp | Ventilator leak compensation |
US11027080B2 (en) | 2008-03-31 | 2021-06-08 | Covidien Lp | System and method for determining ventilator leakage during stable periods within a breath |
US10207069B2 (en) | 2008-03-31 | 2019-02-19 | Covidien Lp | System and method for determining ventilator leakage during stable periods within a breath |
US8434480B2 (en) | 2008-03-31 | 2013-05-07 | Covidien Lp | Ventilator leak compensation |
US8746248B2 (en) | 2008-03-31 | 2014-06-10 | Covidien Lp | Determination of patient circuit disconnect in leak-compensated ventilatory support |
US20130068220A1 (en) * | 2008-09-23 | 2013-03-21 | Ravikumar V. Kudaravalli | Systems and methods for generating liquid oxygen for portable use |
US9889269B2 (en) * | 2008-09-23 | 2018-02-13 | Caire Inc. | Systems and methods for generating liquid oxygen for portable use |
US9556029B2 (en) * | 2008-12-22 | 2017-01-31 | Koninklijke Philips N.V. | Liquid oxygen production device and method |
US20110239698A1 (en) * | 2008-12-22 | 2011-10-06 | Koninklijke Philips Electronics, N.V. | Liquid oxygen production device and method |
US8424521B2 (en) | 2009-02-27 | 2013-04-23 | Covidien Lp | Leak-compensated respiratory mechanics estimation in medical ventilators |
US8978650B2 (en) | 2009-03-20 | 2015-03-17 | Covidien Lp | Leak-compensated proportional assist ventilation |
US8418691B2 (en) | 2009-03-20 | 2013-04-16 | Covidien Lp | Leak-compensated pressure regulated volume control ventilation |
US8973577B2 (en) | 2009-03-20 | 2015-03-10 | Covidien Lp | Leak-compensated pressure regulated volume control ventilation |
US8448641B2 (en) | 2009-03-20 | 2013-05-28 | Covidien Lp | Leak-compensated proportional assist ventilation |
US9841228B2 (en) * | 2009-09-29 | 2017-12-12 | Koninklijke Philips N.V. | System and method for liquefying a fluid and storing the liquefied fluid |
US20160003525A1 (en) * | 2009-09-29 | 2016-01-07 | Koninklijke Philips N.V. | System and method for liquefying a fluid and storing the liquefied fluid |
US11833297B2 (en) | 2011-12-31 | 2023-12-05 | Covidien Lp | Methods and systems for adaptive base flow and leak compensation |
US9550039B2 (en) | 2012-12-04 | 2017-01-24 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US10556082B2 (en) | 2012-12-04 | 2020-02-11 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US9032959B2 (en) | 2012-12-04 | 2015-05-19 | Ino Therapeutics Llc | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US10130783B2 (en) | 2012-12-04 | 2018-11-20 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US9795756B2 (en) | 2012-12-04 | 2017-10-24 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US8770199B2 (en) | 2012-12-04 | 2014-07-08 | Ino Therapeutics Llc | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US10918819B2 (en) | 2012-12-04 | 2021-02-16 | Mallinckrodt Hospital Products IP Limited | Cannula for minimizing dilution of dosing during nitric oxide delivery |
US11235114B2 (en) | 2013-10-18 | 2022-02-01 | Covidien Lp | Methods and systems for leak estimation |
US10207068B2 (en) | 2013-10-18 | 2019-02-19 | Covidien Lp | Methods and systems for leak estimation |
US9675771B2 (en) | 2013-10-18 | 2017-06-13 | Covidien Lp | Methods and systems for leak estimation |
US10343000B2 (en) * | 2015-10-30 | 2019-07-09 | Richard Givens | Oxygen concentrating self-rescuer device |
US20170120085A1 (en) * | 2015-10-30 | 2017-05-04 | Richard Givens | Oxygen concentrating self-rescuer device |
US11305135B2 (en) | 2015-10-30 | 2022-04-19 | Richard Givens | Oxygen concentrating self-rescuer device |
US11873757B1 (en) | 2022-05-24 | 2024-01-16 | Ray E. Combs | System for delivering oxygen to an internal combustion engine of a vehicle |
Also Published As
Publication number | Publication date |
---|---|
US6681764B1 (en) | 2004-01-27 |
CA2293287C (en) | 2005-11-01 |
DE69800669T2 (en) | 2001-11-08 |
JP2002510226A (en) | 2002-04-02 |
JP4729593B2 (en) | 2011-07-20 |
US6698423B1 (en) | 2004-03-02 |
US6651653B1 (en) | 2003-11-25 |
WO1998058219A1 (en) | 1998-12-23 |
EP0990107A1 (en) | 2000-04-05 |
JP4183760B2 (en) | 2008-11-19 |
CA2293287A1 (en) | 1998-12-23 |
US5979440A (en) | 1999-11-09 |
DE69800669D1 (en) | 2001-05-10 |
EP0990107B1 (en) | 2001-04-04 |
JP2008183422A (en) | 2008-08-14 |
ATE200349T1 (en) | 2001-04-15 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
USRE43398E1 (en) | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator | |
US6212904B1 (en) | Liquid oxygen production | |
US20090019886A1 (en) | Method and Apparatus for liquefaction of a Gas | |
AU2005299287B2 (en) | Liquefying and storing a gas | |
US7165422B2 (en) | Small-scale gas liquefier | |
EP2154458A2 (en) | Energy efficient, inexpensive extraction of oxygen from ambient air for portable and home use | |
CN102971593B (en) | Gas liquefaction system and method | |
EP2342518B1 (en) | Systems and methods for generating liquid oxygen for portable use | |
US5582016A (en) | Conditioning and loading apparatus and method for gas storage at cryogenic temperature and supercritical pressure | |
US9395046B2 (en) | Liquid to high pressure gas transfill system and method | |
US20100307635A1 (en) | Liquid to high pressure gas transfill system and method | |
CA2447205C (en) | Cryogenic system for providing industrial gas to a use point | |
JP3306668B2 (en) | Air liquefaction separation method and apparatus | |
AU2022293781A1 (en) | Method and apparatus for separation of helium-3 from helium-4 by means of a cryogenic process |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
FPAY | Fee payment |
Year of fee payment: 12 |