US20060272352A1 - Air separator - Google Patents

Air separator Download PDF

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US20060272352A1
US20060272352A1 US10/550,627 US55062704A US2006272352A1 US 20060272352 A1 US20060272352 A1 US 20060272352A1 US 55062704 A US55062704 A US 55062704A US 2006272352 A1 US2006272352 A1 US 2006272352A1
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oxygen
air
passed
gas
compressed air
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Inventor
Hiroshi Aoki
Akira Yoshino
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Air Water Inc
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Air Water Inc
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Assigned to AIR WATER INC. reassignment AIR WATER INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AOKI, HIROSHI, YOSHINO, AKIRA
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04036—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04636—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a hybrid air separation unit, e.g. combined process by cryogenic separation 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2210/50—Oxygen

Definitions

  • the present invention relates to an air separator capable of producing oxygen gas in an energy-saving manner, thereby remarkable downsizing can be realized.
  • a nitrogen gas (GN 2 ), an oxygen gas (GO 2 ), argon (Ar) and the like are manufactured by the following steps.
  • air is used as a raw material and is compressed by an air compressor 61 and the thus compressed air is put into adsorption towers 62 for eliminating water (H 2 O), carbon dioxide gas (CO 2 ) and hydrocarbon gas (C n M m ) from the compressed air by means of adsorption.
  • the thus obtained gas is passed through a main heat exchanger (not shown) in a cold box 63 so as to be cooled to a super low temperature by heat-exchanging with refrigerant.
  • product gas such as nitrogen gas or oxygen gas
  • product gas is manufactured by cryogenically separating the thus cooled gas in a rectification tower (not shown) and is passed through the main heat exchanger, so that the temperature of the product gas is increased nearly to ambient temperature.
  • An exhaust gas withdrawn from the cold box 63 is used for regenerating the adsorption towers 62 (see, for example, Japanese Unexamined Patent Publication No. 8-261644).
  • a reference numeral 64 indicates a heater for regeneration and evacuation.
  • an air compressor 61 having a discharge pressure of about 5 kg/cm 2 G (0.5 MPaG (gauge pressure)) is generally used.
  • the amount of air required for manufacturing oxygen gas of 10,000 m 3 /h (Normal) by using such an air compressor 61 is calculated as follows. Each rate (% by volume) of elements of air, that is, oxygen, nitrogen and argon, is 20.9%, 78.1% and 0.9%, respectively. When recovery efficiency of oxygen gas is 97%, the amount of air is theoretically calculated by the formula of (10,000 ⁇ 0.209) ⁇ 0.97. As a result, about 50,000 m 3 /h (Normal) is determined as the air required.
  • each of the adsorption towers 62 , the main heat exchanger, the rectification tower and the like should be enlarged correspondingly for such an amount of air, which makes the apparatus large-sized as a whole.
  • the power required for working the air compressor 61 is about 4500 kW (power required for compression is generally considered to be equal to a value found by multiplying the required amount of air by about 0.09), and the power required for working the heater 64 for regeneration and evacuation of the adsorption towers 62 is about 500 kW.
  • a great amount of power of about 5000 kW is required, which means a significant energy required for manufacturing oxygen.
  • the present invention is made in view of such circumstances and it is an object of the invention to provide an air separator capable of manufacturing oxygen gas in an energy-saving manner and that enables cryogenic separation mechanism and the like (a cold box and interior devices therein) to be remarkably downsized.
  • an air separator including an air compression means for taking in air from the outside and compressing it at a low pressure, an oxygen concentrating means for concentrating oxygen gas that is contained in the air compressed by the air compression means, an oxygen/air compression means for further compressing oxygen-rich compressed air (X), which has passed through the oxygen concentrating means, a heat exchanger for cooling oxygen-rich compressed air (Y), which has passed through the oxygen/air compression means, and a rectification tower for taking out oxygen gas by separating the oxygen-rich compressed air (Y), which has passed through the heat exchanger so as to be cooled to a low temperature, by utilizing differences in boiling points of elemental gases.
  • raw-material air is compressed at a low pressure by an air compression means, the concentration of oxygen in the raw-material air is increased by an oxygen concentrating means, following the air compression means, for concentrating oxygen gas in the thus compressed air, the thus obtained gas is passed through an oxygen/air compression means and a heat exchanger, and then is supplied to a rectification tower.
  • low pressure in the above-mentioned context means a pressure lower than the compression pressure caused by the oxygen/air compression means, and means generally not more than one-third, preferably not more than one-fifth, and more preferably not more than one-tenth of the compression pressure by the oxygen/air compression means.
  • the oxygen concentrating means is an adsorption tower accommodating an adsorbent for adsorbing nitrogen gas in the compressed air and impurities such as moisture in the compressed air are adsorbed by the adsorbent
  • the oxygen gas in the compressed air can be concentrated by the action of the adsorbent of the adsorption tower and also moisture in the compressed air can be eliminated so that the resultant gas to be compressed by the oxygen/air compression means following the oxygen concentrating means becomes drier and thus power for compression can further be reduced.
  • an elimination means for eliminating impurities in the oxygen-rich compressed air (Y) is provided between the oxygen/air compression means and the heat exchanger, hydrocarbon, moisture, NO x and the like slightly remaining in the oxygen-rich compressed air (Y) can be eliminated, so that poor-quality air such as air in coastal areas (containing many sodium ions) and air alongside a street (containing much automotive exhaust gas) can be used as a raw-material air.
  • the part of the compressed air directly supplied to the inlet path (after having passed through the air compression means) is allowed to merge into the remaining part of the compressed air supplied to the inlet path (after having passed through the air compression means and introduced into the oxygen concentrating means so as to become the oxygen-rich compressed air (X)), thereby the concentration of oxygen in the oxygen-rich compressed air (X) can be lowered. Therefore, when the amount of oxygen to be manufactured needs to be reduced, it can be realized by adjusting the amount of the compressed air directly supplied to the inlet path.
  • FIG. 1 is a block diagram of one embodiment of an air separator according to the present invention.
  • FIG. 2 is a block diagram of another embodiment of an air separator according to the present invention.
  • FIG. 3 is a block diagram of a further embodiment of an air separator according to the present invention.
  • FIG. 4 is a block diagram of a still further embodiment of an air separator according to the present invention.
  • FIG. 5 is a block diagram of a still further embodiment of an air separator according to the present invention.
  • FIG. 6 is a block diagram of a conventional example.
  • FIG. 1 is a block diagram of one embodiment of an air separator according to the present invention.
  • a reference numeral 1 indicates an air compressor (air compression means) for taking in air and compressing it, wherein a discharge pressure is low and about 0.1 kg/cm 2 G (0.01 MPaG (gauge pressure)).
  • a reference numeral 1 a indicates a first feeding pipe for feeding compressed air passed through the air compressor 1 into first adsorption towers 2 , 3 .
  • the first adsorption towers (oxygen concentration means) 2 , 3 are filled with an adsorbent such as silica gel at an upstream side thereof, and they are also filled with a molecular sieve adsorbent developed by the present applicant (AW0203 available from Air Water Inc.) at a downstream side.
  • the first adsorption towers 2 , 3 are aligned in pairs and one of them works for adsorption while the other works for regeneration, alternately.
  • the amount (% by volume) of each of the components of the low-pressure compressed air passed through the air compressor 1 is arranged, for example, in such a manner that oxygen gas is about 50%, nitrogen gas is about 47.5% and argon gas is about 2.5%, respectively.
  • the concentration of the oxygen gas in the compressed air is increased from 20.9% by volume to 50% by volume.
  • the adsorption towers 2 , 3 also eliminates water (H 2 O), carbon dioxide gas (CO 2 ), hydrocarbon gas (C n M m ) and the like from the compressed air by the action of the adsorbent, simultaneously with the above-mentioned increase in oxygen concentration.
  • a reference numeral 4 indicates a vacuum pump for regeneration and evacuation of the first adsorption towers 2 , 3
  • a reference numeral 4 a indicates a first release pipe for releasing exhaust gas adsorbed by the adsorbent of the first adsorption towers 2 , 3 into the atmosphere and regenerating the adsorbent.
  • the system composed of the first adsorption towers 2 , 3 , and their pipes provided with open-close valves 6 a, 6 b and 8 a, 8 b, respectively, and the vacuum pump 4 is a VSA (vacuum Swing Absorbed) system, which is a membrane separation system, so that one adsorption tower 2 ( 3 ) works for adsorption while the other tower 3 ( 2 ) is regenerated by means of vacuum suction by the vacuum pump 4 .
  • VSA vacuum Swing Absorbed
  • a water separator (not shown) may be provided between the air compressor 1 and the first adsorption towers 2 , 3 for eliminating moisture from the compressed air compressed by the air compressor, and, as required, a flon cooler (not shown) for cooling the compressed air passed through the water separator may be provided.
  • the above-mentioned system is a VSA system, however, it may be a membrane separation system such as a PSA (Pressure Swing Absorbed) system or a TSA (Thermal Swing Absorbed) system.
  • PSA Pressure Swing Absorbed
  • TSA Thermal Swing Absorbed
  • reference numerals 6 a, 6 b, 7 a, 7 b, 8 a and 8 b are open-close valves for conducting adsorption or regeneration of the first adsorption towers 2 , 3 , alternately.
  • a reference numeral 11 indicates a compact oxygen/air compressor (oxygen/air compression means) for further compressing the oxygen-rich compressed air (X) passed through the first adsorption towers 2 , 3 .
  • oxygen/air compressor oxygen/air compression means
  • the oxygen/air compressor can be downsized to a half size or less.
  • a compact oxygen/air compressor oval centrifugal compressor having a discharge pressure of 5 kg/cm 2 G (0.5 MPaG (gauge pressure) for further compressing the oxygen-rich compressed air (X) is used as the compact oxygen/air compressor 11 .
  • the oxygen/air compressor 11 is an oilless mechanism to prevent explosion in further compressing the oxygen-rich compressed air (X).
  • a reference numeral 11 a indicates a second feeding pipe for feeding the oxygen-rich compressed air (Y) passed through the oxygen/air compressor 11 to second adsorption towers 12 , 13 .
  • the adsorption towers 12 , 13 each filled with an adsorbent such as a commercially available molecular sieve, are aligned in pairs and one of them works for adsorption while the other works for regeneration, alternately (and is a compact size of half or less as compared with the conventional type) for eliminating water (H 2 O), carbon dioxide gas, C n M m , NO x and the like slightly remaining in the oxygen-rich compressed air (Y) further compressed by the oxygen/air compressor 11 .
  • a reference numeral 14 indicates a second release pipe for releasing exhaust gas, which has finished the regeneration process in the second adsorption towers 12 , 13 , into the atmosphere.
  • the system composed of the second adsorption towers 12 , 13 , and their pipes provided with open-close valves 16 a, 16 b and 19 a, 19 b, respectively, is a TSA system.
  • reference numerals 16 a, 16 b, 17 a, 17 b, 18 a, 18 b, 19 a and 19 b are open-close valves for conducting adsorption or regeneration of the second adsorption towers 12 , 13 , alternately.
  • a reference numeral 21 indicates a main heat exchanger such as a plate-fin exchanger, which cools the oxygen-rich compressed air (Y), wherein minute amounts of water, carbon dioxide gas and the like remaining are eliminated by means of adsorption by adsorption towers 12 , 13 , to a super low temperature.
  • the main heat exchanger 21 can be downsized to a half size or less.
  • a reference numeral 22 indicates a supply pipe for supplying the oxygen-rich compressed air (Y) cooled to a super low temperature by the main heat exchanger 21 into a lower part of a high-pressure rectification tower 23 .
  • the high-pressure rectification tower 23 As the amount of gas to be circulated through the high-pressure rectification tower (a column plate type or a packed column type) 23 can be halved as compared with that of the conventional type, the half or less capacity of the high-pressure rectification tower is enough and thus the size thereof can be downsized to half or less.
  • liquid oxygen-rich liquid air 24 of the oxygen-rich compressed air (Y) fed through the supply pipe 22 accumulates in the bottom portion, while nitrogen gas rises.
  • a part of the rising nitrogen gas is passed through a first reflux pipe 31 and introduced into a condenser 30 positioned in a lower portion of a low-pressure rectification tower 28 , while the remaining part thereof is passed through a nitrogen takeout pipe 26 and activates an expansion turbine 37 .
  • the nitrogen gas introduced into the condenser 30 is liquefied so as to become liquid nitrogen.
  • the nitrogen gas thus liquefied is returned through a second reflux pipe 32 to an upper portion of the high-pressure rectification tower 23 as a reflux liquid, and flows downward in the high-pressure rectification tower 23 , and then contacts in a countercurrent manner the oxygen-rich compressed air (Y) rising from the bottom, thereby liquefying a high-boiling point elemental gas (oxygen gas) in the oxygen-rich compressed air (Y), which flows downward.
  • oxygen gas oxygen gas
  • the liquid oxygen-rich liquid air 24 is accumulated in the bottom so as to be further oxygen-rich, while a low-boiling elemental gas (nitrogen gas) rises upward in the high-pressure rectification tower 23 .
  • the nitrogen gas withdrawn through the nitrogen takeout pipe 26 is supplied to the main heat exchanger 21 so as to cool compressed air passed through the main heat exchanger 21 , and is supplied through a first connecting pipe 26 a to an expansion turbine 37 so as to be a driving source for the expansion turbine 37 , as mentioned above, to generate cold.
  • a reference numeral 38 indicates a bypass provided with an open-close valve 38 a.
  • the nitrogen gas introduced through the nitrogen takeout pipe 26 and the first connecting pipe 26 a provided with the open-close valve 26 b into the expansion turbine 37 expands therein and conducts thermodynamic external work, so that the nitrogen gas is cooled to an extremely low temperature to generate cold in an amount required for the air separator.
  • the nitrogen gas in such a state is supplied through a second connecting pipe 37 a into the main heat exchanger 21 wherein the nitrogen gas itself becomes ambient temperature by heat exchanging with a raw material air for imparting the cold to the raw material air.
  • Most of such nitrogen gas is passed through a release pipe 37 b and is released into the atmosphere as an exhaust gas, while a part thereof is passed through a branch pipe 40 so as to regenerate an adsorbent of the second adsorption towers 12 , 13 .
  • the branch pipe 40 functions for supplying the introduced nitrogen gas into either a first pipe 42 provided with a heater 41 or a second pipe 43 without a heater.
  • a reference numeral 44 indicates a third pipe for supplying nitrogen gas passed through the first pipe 42 or the second pipe 43 into the second adsorption towers 12 , 13 for regenerating the adsorbent.
  • a reference numeral 28 indicates a low-pressure rectification tower (a column plate type or a packed column type) located above the high-pressure rectification tower 23 .
  • the liquid oxygen-rich liquid air 24 accumulated in the bottom of the high-pressure rectification tower 23 is fed through a feeding pipe 29 provided with an expansion valve 29 a into the low-pressure rectification tower 28 .
  • the low-pressure rectification tower 28 contains the condenser 30 in the bottom thereof into which a part of nitrogen gas withdrawn from the high-pressure rectification tower 23 is introduced through the first reflux pipe 31 .
  • liquid oxygen 34 (LO 2 : purity of about 99.7% by volume) accumulated in the bottom of the low-pressure rectification tower 28 so as to be evaporated while the nitrogen itself liquefies due to coldness of the liquid oxygen 34 and a part thereof is returned through the second reflux pipe 32 provided with a flow adjusting valve 32 a to the upper part of the high-pressure rectification tower 23 as a reflux liquid, as mentioned above.
  • the remaining part of the liquid nitrogen 34 is introduced through a branch pipe 33 provided with a flow adjusting valve 33 a into the upper part of the low-pressure rectification tower 28 as a reflux liquid and flows down through the low-pressure rectification tower 28 for gas-liquid separation.
  • a reference numeral 35 indicates a product oxygen gas takeout pipe extended from the lower part of the low-pressure rectification tower 28 .
  • the product oxygen gas takeout pipe 35 takes out high-purity oxygen gas evaporated from the liquid oxygen 34 accumulated in the bottom of the low-pressure rectification tower 28 and feeds the thus withdrawn oxygen gas to the main heat exchanger 21 for heat-exchange with the oxygen-rich compressed air (Y) so that the oxygen gas itself becomes ambient temperature and then is released to the outside of the apparatus as product oxygen.
  • a reference numeral 36 indicates a product nitrogen gas takeout pipe extended from the upper part of the low-pressure rectification tower 28 .
  • the product nitrogen gas takeout pipe 36 takes out nitrogen gas rising upwards in the low-pressure rectification tower 28 and feeds the thus withdrawn nitrogen gas to the main heat exchanger 21 for cooling the oxygen-rich compressed air (Y), so that the nitrogen gas itself becomes ambient temperature and then is released to the outside of the apparatus as product nitrogen gas.
  • a reference numeral 39 is a cold box into which heat insulating material such as perlite (not shown) is packed for low-temperature insulation.
  • oxygen is concentrated by adsorbing nitrogen gas in the first adsorption towers 2 , 3 , however, an adsorbent for adsorbing oxygen gas may be used, so that oxygen gas may be adsorbed, and the thus obtained oxygen gas is concentrated, and then withdrawn.
  • the nitrogen gas and the oxygen gas are manufactured by using this apparatus in the following manner. That is, air is taken into the air compressor (air compression means) 1 from the outside so as to be compressed at a low pressure, and moisture in the compressed air is eliminated by the water separator (not shown), and then the air in such a state is fed into the first adsorption towers (oxygen concentrating means) 2 , 3 , so that nitrogen gas, moisture, carbon dioxide gas, hydrocarbon gas (C n M m ) and the like from the compressed air are eliminated by means of adsorption, thereby oxygen gas in the compressed air is concentrated, which is a main feature of the present invention.
  • the oxygen-rich compressed air (X) from the first adsorption towers 2 , 3 is introduced into the oxygen/air compressor (oxygen/air compression means) 11 for further compressing the oxygen-rich compressed air (X) for obtaining the oxygen-rich compressed air (Y).
  • the oxygen-rich compressed air (Y) is fed into the second adsorption towers 12 , 13 for eliminating water, carbon dioxide gas, NO x and the like in the oxygen-rich compressed air (Y)
  • the oxygen-rich compressed air (Y) from which water, carbon dioxide gas, No x and the like have been eliminated by adsorption, is fed into the main heat exchanger 21 so as to be cooled to a super low temperature, and is introduced into the lower part of the high-pressure rectification tower 23 in such a state.
  • the oxygen-rich compressed air (Y) is brought into contact with reflux liquid produced in the low-pressure rectification tower 28 in a countercurrent manner for purifying the compressed air, thereby liquefying a high-boiling point elemental gas (oxygen gas) in the oxygen-rich compressed air (Y), thereby leaving nitrogen in a gaseous state by using the difference in boiling point between nitrogen and oxygen (boiling point for oxygen of ⁇ 183° C., that for nitrogen of ⁇ 196° C.).
  • the nitrogen gas is withdrawn through the nitrogen takeout pipe 26 , and is supplied to the main heat exchanger 21 , and then is supplied to the expansion turbine 37 so as to generate cold. Most of such nitrogen gas is released to the outside of the apparatus while a part thereof is used for regenerating the second adsorption towers 12 , 13 .
  • nitrogen gas accumulated in the upper part of the low-pressure rectification tower 28 is taken out through the product nitrogen gas takeout pipe 36 is fed into the main heat exchanger 21 so as to be heated nearly to the ambient temperature, and then released to the outside of the apparatus as product nitrogen gas.
  • the liquid oxygen-rich liquid air 24 accumulated in the bottom of the high-pressure rectification tower 23 is fed through a feeding pipe 29 into the low-pressure rectification tower 28 , and liquid oxygen 34 , wherein nitrogen has been evaporated and eliminated, is accumulated in the bottom of the low-pressure rectification tower 28 and is heat exchanged with nitrogen gas passed through the condenser 30 positioned in the bottom of the low-pressure rectification tower 28 so as to be evaporated.
  • the thus evaporated oxygen gas is withdrawn through the product gas takeout pipe 35 , and is fed into the main heat exchanger 21 so as to be heated nearly to the ambient temperature, and then is released to the outside of the apparatus as a product oxygen gas.
  • product oxygen gas and product nitrogen gas can be obtained.
  • the concentration of oxygen in the compressed air is increased from 20.9% by volume to about 50% by volume by the first adsorption towers 2 , 3 .
  • the amount of air required for manufacturing oxygen gas of 10,000 m 3 /h (Normal) is calculated as follows. When recovery efficiency of oxygen gas is 97%, the amount of air is theoretically calculated by the formula of (10,000 ⁇ 0.500) ⁇ 0.97. As a result, about 20,600 m 3 /h (Normal) is determined as the air required, which is reduced to about 41% as compared with that required in the conventional apparatus mentioned at the beginning of the present specification.
  • the power required for working the oxygen/air compressor 11 is reduced to about 2000 kW, and it is thought that the power required for working the oxygen/air compressor 1 is about 300 kW, the power required for working the vacuum pump 4 is about 900 kW, and the electrical power for the electrical heater 41 is about 200 kW.
  • the total amount is about 3400 kW, reduced to about 70% as compared with the conventional apparatus. Therefore, energy can be saved by 30% or more.
  • the first adsorption towers 2 , 3 are provided for increasing the concentration of the oxygen gas in the compressed air obtained by compressing air as raw material by the air compressor 1 .
  • the thus obtained gas is fed through the oxygen/air compressor 11 and the main heat exchanger 21 into the high-pressure rectification tower 23 and the low-pressure rectification tower 28 .
  • the amount of gas to be circulated through each device such as the main heat exchanger 21 and both of the rectification towers 23 , 28 following the oxygen/air compressor 11 , can be reduced, so that each device can be downsized to a half size or less, which enables remarkable downsizing of the entire apparatus.
  • the high-pressure rectification tower 23 has a diameter of 7 m in the conventional apparatus (according to the calculated value by the applicant). Since there is no means for transporting such a high-pressure rectification tower, there is no choice but to assemble it on site. However, when the same amount of oxygen gas is produced in this embodiment, the amount of gas to be circulated through the rectification tower can be halved, so that the diameter of the rectification tower can be reduced to about 4.2 m. For this reason, it is possible to transport the rectification tower assembled in a plant to a site, resulting in great laborsaving.
  • FIG. 2 illustrates another embodiment of an air separator according to the present invention.
  • second adsorption towers 12 , 13 are eliminated.
  • second adsorption towers 12 , 13 a second release pipe 14 , pipes provided with open-close valves 16 a, 16 b, 17 a, 17 b, 18 a, 18 b, 19 a and 19 b, a branch pipe 40 , first to third pipes 42 to 44 are eliminated.
  • this embodiment is the same as the above-mentioned embodiment and similar parts are denoted by the same reference numerals.
  • FIG. 3 illustrates a further embodiment of an air separator according to the present invention.
  • a liquid oxygen tank (not shown) into which liquid oxygen (LO 2 ) is supplied from the outside of the apparatus by means of a tanker or the like is used instead of an expansion turbine 37 in the embodiment as shown in FIG. 2 .
  • LO 2 liquid oxygen
  • this embodiment is substantially the same as that shown in FIG. 2 .
  • a reference numeral 47 indicates an inlet pipe for introducing the liquid oxygen from the liquid oxygen tank into the lower part of a low-pressure rectification tower 28 as a cold source.
  • a reference numeral 48 indicates an exhaust pipe extended from the low-pressure rectification tower 28 for withdrawing nitrogen gas (exhaust GN 2 ) accumulated in the upper part of each shelf (or packed column) of the low-pressure rectification tower 28 so as to be introduced into a supercooler 49 .
  • the exhaust pipe 48 leads the exhaust nitrogen gas passed through the supercooler 49 into a main heat exchanger 21 for cooling the oxygen-rich compressed air (Y) and releases the exhaust nitrogen gas to the outside.
  • the supercooler 49 through which are passed: a) oxygen-rich liquid air 24 via a feeding pipe 29 ; b) liquid nitrogen (reflux liquid) via a branch pipe 33 ; c) product nitrogen gas via a product nitrogen gas takeout pipe 36 ; and d) exhaust nitrogen gas via the exhaust pipe 48 , works for cooling the oxygen-rich liquid air 24 a).
  • a reference numeral 50 indicates a liquid oxygen takeout pipe extended from the bottom of the low-pressure rectification tower 28 .
  • the liquid oxygen takeout pipe 50 takes out liquid oxygen accumulated in the bottom of the low-pressure rectification tower 28 , which is led into the main heat exchanger 21 for cooling the oxygen-rich compressed air (Y), and also heating the liquid oxygen itself up to ambient temperature for obtaining product oxygen gas, and introduces the thus obtained product oxygen gas into a product oxygen gas takeout pipe 35 .
  • a reference numeral 51 indicates a product nitrogen gas compressor installed in a product nitrogen takeout pipe 36 for increasing the pressure of the product nitrogen gas passing through the product nitrogen gas takeout pipe 36 to a specified pressure.
  • a reference numeral 52 indicates a first product oxygen gas compressor installed in the product oxygen gas takeout pipe 35 for increasing the pressure of the product oxygen gas passing through the product oxygen gas takeout pipe 35 to a specified pressure and feeding the product oxygen gas into a low pressure product oxygen gas takeout pipe 53 .
  • a reference numeral 54 indicates a second product oxygen gas compressor for further increasing the pressure of the product oxygen gas passed through the first product oxygen gas compressor 52 and feeding the product oxygen gas into a high pressure product oxygen gas takeout pipe 55 .
  • the ceiling of the high-pressure rectification tower 23 and the bottom of the low-pressure rectification tower 28 located above the high-pressure rectification tower 23 are formed integrally by the same material. In FIG.
  • a reference numeral 36 a indicates a pipe for feeding a product nitrogen gas passing through the product nitrogen takeout pipe 36 into an exhaust pipe 48 .
  • a reference numeral 39 A is a cold box in which an insulating material such as perlite is filled and vacuum sucked. Except for that, this embodiment is the same as that shown in FIG. 2 and similar parts are denoted by the same reference numerals.
  • the nitrogen gas and the oxygen gas are manufactured by using this apparatus in the following manner. That is, in the same manner as in the embodiment as shown in FIG. 2 , air is taken into the air compressor (air compression means) 1 from the outside in which air is compressed at a low pressure, and moisture in the compressed air is eliminated by the water separator (not shown), and then the air in such a state is fed into the first adsorption towers (oxygen concentrating means) 2 , 3 , so that nitrogen gas, moisture, carbon dioxide gas, hydrocarbon gas (C n M m ) and the like in the compressed air are eliminated by means of adsorption, thereby the concentration of oxygen gas in the compressed air is increased.
  • the oxygen-rich compressed air (X) from the first adsorption towers 2 , 3 is introduced into the oxygen/air compressor (oxygen/air compression means) 11 for further compressing the oxygen-rich compressed air (X) for obtaining the oxygen-rich compressed air (Y).
  • the oxygen-rich compressed air (Y) is fed into the main heat exchanger 21 to be cooled to a super low temperature and is introduced into a lower part of a high-pressure rectification tower 23 in such a state.
  • the oxygen-rich compressed air (Y) is brought into contact with reflux liquid produced in the low-pressure rectification tower 28 in a countercurrent manner for purifying the compressed air, thereby liquefying a high-boiling point elemental gas (oxygen gas) in the oxygen-rich compressed air (Y), thereby leaving nitrogen in a gaseous state by using the difference in boiling point between nitrogen and oxygen (boiling point for oxygen of ⁇ 183° C., that for nitrogen of ⁇ 196° C.)
  • nitrogen gas accumulated in the upper part of the low-pressure rectification tower 28 is taken out through the product nitrogen gas takeout pipe 36 , and is fed into the supercooler (heat exchanger) 49 , and then is fed into the main heat exchanger 21 so as to be heated nearly to the ambient temperature, and finally is released to the outside of the apparatus as product nitrogen gas.
  • the oxygen-rich liquid air 24 accumulated in the bottom of the high-pressure rectification tower 23 is fed through a feeding pipe 29 into the supercooler 49 so as to be cooled.
  • the oxygen-rich liquid air 24 in a gas-liquid mixing state is fed into the low-pressure rectification tower 28 , wherein nitrogen has been evaporated and eliminated, so that liquid oxygen 34 is accumulated in the bottom of the low-pressure rectification tower 28 and is heat exchanged with nitrogen gas passed through the condenser 30 positioned in the bottom of the low-pressure rectification tower 28 so as to be evaporated.
  • the thus evaporated oxygen gas is withdrawn through the product oxygen gas takeout pipe 35 , and is fed into the main heat exchanger 21 so as to be heated nearly to the ambient temperature, and then is released through a low-pressure product oxygen gas takeout pipe 53 via a first product oxygen gas compressor 52 to the outside of the apparatus as product oxygen gas and is also released through a high-pressure product oxygen takeout pipe 55 via a second product oxygen gas compressor 54 to the outside of the apparatus as product oxygen gas.
  • the product oxygen gas and the product nitrogen gas can be obtained.
  • FIG. 4 illustrates a still further embodiment of an air separator according to the present invention.
  • a liquid nitrogen tank (not shown) into which liquid nitrogen (LN z ) is supplied from the outside of the apparatus by means of a tanker or the like is used instead of an expansion turbine 37 in the embodiment as shown in FIG. 2 .
  • this embodiment is substantially the same as that shown in FIG. 2 .
  • a reference numeral 47 a indicates an inlet pipe for introducing the liquid nitrogen from the liquid nitrogen tank into the upper part of a high-pressure rectification tower 23 as a cold source.
  • FIG. 5 illustrates a still further embodiment of an air separator according to the present invention.
  • the first feeding pipe 1 a for feeding the compressed air which has passed through the air compressor 1 into first adsorption towers 2 , 3 and an inlet pipe 57 (a reference numeral 57 is not denoted in FIG. 1 ) for introducing the oxygen-rich compressed air (X), which has passed through the first adsorption towers 2 , 3 , into the oxygen/air compressor 11 (as in the embodiment as shown in FIG. 1 ) are connected with a connecting pipe 58 provided with an open-close valve (or a flow adjusting valve) 58 a.
  • a part of the compressed air which has passed through the air compressor 1 and a water separator (not shown) is fed directly through the connecting pipe 58 into the inlet pipe 57 by opening the open-close valve 58 a (i.e., instead of being passed through the adsorption towers 2 , 3 ), and the remaining part is passed through the adsorption towers 2 , 3 and introduced into the inlet pipe 57 , so that both are allowed to join in the inlet pipe 57 .
  • the concentration of the oxygen gas of the remaining part of the compressed air introduced through the first adsorption towers 2 , 3 into the inlet pipe 57 is diluted with the part of the compressed air introduced through the connecting pipe 58 into the inlet pipe 57 .
  • this embodiment is the same as that shown in FIG. 1 and similar parts are denoted by the same reference numerals. The same effects and advantages are obtained in this embodiment as well as in the embodiment as shown in FIG. 1 . Further, since the concentration of the oxygen gas in the compressed air supplied into the lower part of the high-pressure rectification tower 23 is lowered, the amount of the product oxygen gas can be reduced. Therefore, when the amount of the product oxygen gas is needed to be reduced, this embodiment enables to reduce it, correspondingly.
  • Such a connecting pipe 58 provided with an open-close valve 58 a can be used in the embodiments as shown in FIG. 2 to FIG. 4 .

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Drying Of Gases (AREA)
US10/550,627 2003-03-26 2004-03-25 Air separator Abandoned US20060272352A1 (en)

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JP2003086052 2003-03-26
JP2003086052 2003-03-26
JP2004002877A JP4782380B2 (ja) 2003-03-26 2004-01-08 空気分離装置
JP2004002877 2004-01-08
PCT/JP2004/004145 WO2004085941A1 (ja) 2003-03-26 2004-03-25 空気分離装置

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JP (1) JP4782380B2 (pt)
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090223247A1 (en) * 2005-06-23 2009-09-10 Air Water Inc. Method of generating nitrogen and apparatus for use in the same
US9144767B2 (en) * 2012-06-19 2015-09-29 Tokyo Gas Co., Ltd. Gas separation device
US20210095922A1 (en) * 2016-03-25 2021-04-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression
CN114558416A (zh) * 2022-01-24 2022-05-31 湖南泰瑞医疗科技有限公司 一种集成节能制氧系统

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2911391A1 (fr) * 2007-01-16 2008-07-18 Air Liquide Procede de separation utilisant une colonne a garnissage structure ondule-croise pour la separation d'un melange de gaz et colonne adaptee a etre utilisee pour le procede
KR100930316B1 (ko) * 2008-05-16 2009-12-08 대성산업가스 주식회사 초소형 액체질소 및 액체산소 제조장치
JP2013212474A (ja) * 2012-04-03 2013-10-17 Jfe Engineering Corp 気体分離装置
KR101644244B1 (ko) * 2014-11-13 2016-08-11 참좋은우리 주식회사 온습도 조절 장치를 갖춘 오존크림 제조장치를 이용하는 제조방법
KR101644245B1 (ko) * 2014-11-13 2016-08-11 참좋은우리 주식회사 온습도 조절 장치를 갖춘 제조장치에 의해 제조되는 오존크림
CN104534812B (zh) * 2015-01-04 2016-10-19 中煤能源黑龙江煤化工有限公司 一种应用于气体深冷分离设备主精馏塔
KR101683839B1 (ko) * 2015-05-21 2016-12-08 참좋은우리 주식회사 오존크림 고속 제조장치
CN104833174B (zh) * 2015-05-26 2017-08-11 杭州杭氧股份有限公司 一种带压辅助氧塔低能耗生产带压低纯氧和高纯氧产品的装置及方法
JP6575499B2 (ja) * 2016-12-15 2019-09-18 Ｊｆｅスチール株式会社 製鉄プロセスにおける酸素供給装置およびその方法
KR102092716B1 (ko) * 2017-12-07 2020-03-24 주식회사 포스코 공기분리설비
KR102259807B1 (ko) 2019-07-02 2021-06-03 주식회사 포스코 흡착장치 및 이를 갖는 공기분리설비
WO2024010756A1 (en) * 2022-07-08 2024-01-11 Entegris, Inc. Methods and equipment for cryogenic removal of impurities from oxygen gas
CN115451655B (zh) * 2022-09-29 2023-04-28 北京飞燕石化环保科技发展有限公司 一种空分装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2699047A (en) * 1950-10-27 1955-01-11 Linde Eismasch Ag Process for cooling and purifying compressed gas mixtures
US4113839A (en) * 1976-10-29 1978-09-12 Matsushita Electric Industrial Co., Ltd. Nitrogen oxides removal method
US6319303B1 (en) * 1999-10-25 2001-11-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for purifying a gas and corresponding system

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1457882A (en) * 1972-01-07 1976-12-08 Boc International Ltd Air separation
JPS5326276A (en) * 1976-08-25 1978-03-10 Hitachi Ltd Liquefying separation method of air
GB2080929B (en) * 1980-07-22 1984-02-08 Air Prod & Chem Producing gaseous oxygen
JPS6124970A (ja) * 1984-07-13 1986-02-03 大同酸素株式会社 高純度酸素ガス製造装置
JPH0721378B2 (ja) * 1985-08-12 1995-03-08 大同ほくさん株式会社 酸素ガス製造装置
JPH0792332B2 (ja) * 1987-12-28 1995-10-09 日本酸素株式会社 低純度酸素製造方法
DE4109945A1 (de) * 1991-03-26 1992-10-01 Linde Ag Verfahren zur tieftemperaturzerlegung von luft
JP3345508B2 (ja) * 1994-03-31 2002-11-18 住友精密工業株式会社 吸着装置
JPH08291967A (ja) * 1995-04-20 1996-11-05 Daido Hoxan Inc 空気分離方法およびそれに用いる装置
US5701763A (en) * 1997-01-07 1997-12-30 Praxair Technology, Inc. Cryogenic hybrid system for producing low purity oxygen and high purity nitrogen
FR2774308B1 (fr) * 1998-02-05 2000-03-03 Air Liquide Procede et installation combines de production d'air comprime et d'au moins un gaz de l'air
JP4150102B2 (ja) * 1998-05-20 2008-09-17 大陽日酸株式会社 空気液化分離方法及び装置
US6192707B1 (en) * 1999-11-12 2001-02-27 Praxair Technology, Inc. Cryogenic system for producing enriched air

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2699047A (en) * 1950-10-27 1955-01-11 Linde Eismasch Ag Process for cooling and purifying compressed gas mixtures
US4113839A (en) * 1976-10-29 1978-09-12 Matsushita Electric Industrial Co., Ltd. Nitrogen oxides removal method
US6319303B1 (en) * 1999-10-25 2001-11-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for purifying a gas and corresponding system

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090223247A1 (en) * 2005-06-23 2009-09-10 Air Water Inc. Method of generating nitrogen and apparatus for use in the same
US8549878B2 (en) * 2005-06-23 2013-10-08 Air Water Inc. Method of generating nitrogen and apparatus for use in the same
US9144767B2 (en) * 2012-06-19 2015-09-29 Tokyo Gas Co., Ltd. Gas separation device
US20210095922A1 (en) * 2016-03-25 2021-04-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression
US11619443B2 (en) * 2016-03-25 2023-04-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression
CN114558416A (zh) * 2022-01-24 2022-05-31 湖南泰瑞医疗科技有限公司 一种集成节能制氧系统

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CN1764813A (zh) 2006-04-26
CN100390481C (zh) 2008-05-28
BRPI0408715A (pt) 2006-03-07
EP1612496B1 (en) 2016-12-07
JP2004309119A (ja) 2004-11-04
WO2004085941A1 (ja) 2004-10-07
JP4782380B2 (ja) 2011-09-28
KR20060024352A (ko) 2006-03-16
EP1612496A1 (en) 2006-01-04
KR101099855B1 (ko) 2011-12-28
EP1612496A4 (en) 2012-08-29

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Owner name: AIR WATER INC., JAPAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:AOKI, HIROSHI;YOSHINO, AKIRA;REEL/FRAME:018100/0716

Effective date: 20060809

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION