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WO2004085941A1 - Air separator - Google Patents

Air separator Download PDF

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Publication number
WO2004085941A1
WO2004085941A1 PCT/JP2004/004145 JP2004004145W WO2004085941A1 WO 2004085941 A1 WO2004085941 A1 WO 2004085941A1 JP 2004004145 W JP2004004145 W JP 2004004145W WO 2004085941 A1 WO2004085941 A1 WO 2004085941A1
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WO
WIPO (PCT)
Prior art keywords
oxygen
air
compressed air
gas
concentration
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.)
Ceased
Application number
PCT/JP2004/004145
Other languages
French (fr)
Japanese (ja)
Inventor
Hiroshi Aoki
Akira Yoshino
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Water Inc
Original Assignee
Air Water Inc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
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First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=33100392&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2004085941(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Air Water Inc filed Critical Air Water Inc
Priority to BRPI0408715-1A priority Critical patent/BRPI0408715A/en
Priority to KR1020057017678A priority patent/KR101099855B1/en
Priority to EP04723340.8A priority patent/EP1612496B1/en
Priority to CNB2004800080462A priority patent/CN100390481C/en
Priority to US10/550,627 priority patent/US20060272352A1/en
Publication of WO2004085941A1 publication Critical patent/WO2004085941A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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 separation device that can produce oxygen gas with energy saving and that can significantly reduce the size of the device.
  • nitrogen gas (GN 2 ), oxygen gas (G ( 2 ), argon (Ar), etc. are obtained by using air as a raw material, compressing it with an air compressor 61, and adsorbing it.
  • the waste gas extracted from the cold box 63 is used for regeneration of the adsorption tower 6 (see, for example, Japanese Patent Application Laid-Open No. 8-261644).
  • reference numeral 64 denotes a heater for
  • an air compressor 61 having a discharge pressure of about 5 kg / cm 2 G CO. 5 MPag (gauge pressure) is usually used as the air compressor 61.
  • adsorption tower 62 For this reason, it is necessary to use an adsorption tower 62, a main heat exchanger, a rectification tower, and the like corresponding to the required air amount, and the entire apparatus becomes large-scale. Moreover, it produces oxygen gas of 10,000 m 3 / h (No rma 1). In this case, the necessary compression power of the air compressor 61 (this compression power is usually a value obtained by multiplying the above required air amount by about 0.09) Power 500 k
  • the power of the heater 64 for regeneration and exhaust of the adsorption tower 62 is about 500 kW, so a large power of about 500 kW is required, It requires a lot of energy for manufacturing.
  • the present invention has been made in view of such circumstances, and provides an air separation device that can produce oxygen gas with energy saving and that can greatly reduce the size of a cryogenic separation mechanism (a cold box and its internal equipment). For that purpose. Disclosure of the invention
  • an air separation device of the present invention includes an air compression unit that takes in air from the outside and compresses it at a low pressure, and enriches oxygen gas in compressed air compressed by the air compression unit.
  • Oxygen condensing means oxygen-air compression means for further compressing the high-concentration oxygen-containing compressed air X passed through the oxygen concentrating means, and heat exchanger for cooling the high-concentration oxygen-containing compressed air Y passed through the oxygen-air compression means
  • a rectification column for separating the high-concentration oxygen-containing compressed air Y cooled to a low temperature via the heat exchanger by utilizing the boiling point difference of each component gas to take out the oxygen gas.
  • the air separation device of the present invention compresses the raw material air to a low pressure by the air compressing means, and provides the oxygen condensing means for concentrating the oxygen gas in the compressed air following the air compressing means.
  • the oxygen concentration is increased, and this is supplied to the rectification column via oxygen-air compression means and a heat exchanger. Therefore, when producing the same amount of oxygen gas, etc., it is possible to save a large amount of energy and realize a significant reduction in the flow rate of each means after the oxygen enrichment means, thereby reducing them to more than half that of the conventional method.
  • the device can be downsized, and consequently the entire device can be significantly reduced in size.
  • the low pressure refers to a pressure lower than the compression pressure of the oxygen-air compression means, and is usually 1/3 or less, preferably 1/5 or less, more preferably 1/3 of the compression pressure of the oxygen-air compression means. Means less than 1/10.
  • the oxygen concentrating means is an adsorption tower containing an adsorbent for adsorbing nitrogen gas in the compressed air, and the adsorbent removes impurities such as moisture in the compressed air.
  • the oxygen gas in the compressed air can be concentrated by the action of the adsorbent of the adsorption tower and the moisture in the compressed air can also be removed.
  • the object to be compressed with is dried and the compression power can be further reduced.
  • a removing means for removing impurities in the high-concentration oxygen-containing compressed air Y is provided between the oxygen-air compression means and the heat exchanger, a trace amount remains in the high-concentration oxygen-containing compressed air Y. It can remove hydrocarbons, minerals, ⁇ ⁇ ⁇ , etc., and can use poor air such as air along the coast (a lot of sodium ions) or air along the road (a lot of exhaust gas from automobiles) as raw material air. Become like
  • a part of the compressed air compressed by the air compression means is introduced into the introduction path for introducing the high-concentration oxygen-containing compressed air X having passed through the oxygen concentration means to the oxygen-air compression means without passing through the oxygen concentration means.
  • a part of the compressed air which is directly supplied to the above-mentioned introduction path after passing through the air compressing means and is introduced into the oxygen concentrating means after passing through the air compressing means and contains high-concentration oxygen.
  • the remaining portion of the compressed air supplied to the introduction path as the compressed air X is merged in the introduction path, whereby the oxygen concentration in the high-concentration oxygen-containing compressed air X can be reduced.
  • the amount of compressed air supplied directly to the above-mentioned introduction passage can be adjusted to cope with it.
  • FIG. 1 is a configuration diagram showing one embodiment of the air separation device of the present invention
  • FIG. 2 is a configuration diagram showing another embodiment of the air separation device of the present invention
  • Fig. 4 is a configuration diagram showing still another embodiment of the air separation device of the present invention
  • Fig. 4 is a configuration diagram showing still another embodiment of the air separation device of the present invention
  • FIG. 5 is a configuration diagram showing still another embodiment of the air separation device of the present invention
  • FIG. 6 is a configuration diagram showing a conventional example.
  • FIG. 1 shows an embodiment of the air separation device of the present invention.
  • 1 is It is an air compressor (air compression means) that takes in the air and compresses it.
  • air compressor air compression means
  • Reference numeral 1a denotes a first feed pipe for feeding the compressed air that has passed through the air compressor 1 to the first P connecting towers 2 and 3.
  • the first adsorption tower (oxygen concentrating means) 2 and 3 has an upstream side filled with an adsorbent such as silica gel on the upstream side, and a molecular sieve adsorbent (air / air) developed by the applicant on the downstream side.
  • AW 02 03 manufactured by War Yuichisha.
  • the first adsorption towers 2 and 3 are paired and operated by alternately switching between adsorption and regeneration.
  • the component ratio (volume%) of each component gas in the low-pressure compressed air passed through the air compressor 1 is calculated as follows.
  • oxygen gas 50%: nitrogen gas 47.5%: argon gas is about 2.5%
  • concentration of oxygen gas in compressed air is increased from 20.9% by volume to 50% by volume.
  • Reference numeral 4 denotes a vacuum pump for regenerating and exhausting the first adsorption towers 2 and 3
  • reference numeral 4a denotes a first discharge pipe for removing waste gas adsorbed by the adsorbents of the first adsorption towers 2 and 3 to the atmosphere.
  • the system consisting of the first adsorption towers 2, 3 and the pipe lines with the on-off valves 6a, 6b, 8a, 8b and the vacuum pump 4 is constructed as follows. , VS A (vacuum swing absolute), membrane separation, and when one of the first adsorption towers 2 (3) is performing adsorption operation, the other first adsorption tower 3 (2) is vacuum pumped. It is regenerated by the vacuum suction of the pump 4.
  • a water separator (not shown) is provided for cooling the compressed air that has passed through the water separator, if necessary. Is VS A, but PSA (Pressure Swing Absorbed), T
  • Reference numerals 6a, 6b, 7a, 7b, 8a, and 8b denote on-off valves for alternately adsorbing and regenerating the first adsorption towers 2 and 3.
  • the oxygen-air compressor 11 is a small-sized oxygen-air compressor (oil-less centrifugal compressor: discharge pressure 5 kg / cm2) that further compresses the high-concentration oxygen-containing compressed air X.
  • An oxygen air compressor of about 2 G [0.5MPaG (gauge pressure)] is used.
  • the oxygen-air compressor 11 has an oil-less mechanism or the like in order to prevent explosion when compressing the high-concentration oxygen-containing compressed air X further.
  • Reference numeral 11a denotes a second supply pipe for supplying the high-concentration oxygen-containing compressed air Y having passed through the oxygen-air compressor 11 to the second adsorption towers 12, 13. 12 and 13 are filled with an adsorbent such as a commercially available molecular sieve, and alternately adsorb and regenerate.
  • an adsorbent such as a commercially available molecular sieve, and alternately adsorb and regenerate.
  • a set of two small second adsorption towers (smaller than the conventional ones) a summer in which) the size, action for adsorbing and removing water traces remaining on hyperoxia-containing compressed air Y which further compressed by the oxygen pressure compressor 1 1, carbon dioxide, a C n M ra and NO x, etc. do.
  • Reference numeral 14 denotes a second discharge pipe, which discharges waste gas that has been regenerated in the second adsorption towers 12, 13 to the atmosphere.
  • the system including the pipe lines with the second adsorption towers 12, 13 and the on-off valves 16a, 16b, 19a, 19b is TSA.
  • 1 6 a, 1 6 b , 1 7 a, 1 7 b, 18 a, 18 b, 1 9 a s 19 b is for adsorbing 'regeneration operation alternately second adsorption tower 12, 1 3 It is an on-off valve.
  • Reference numeral 22 denotes a supply pipe for sending the high-concentration oxygen-containing compressed air Y cooled to an extremely low temperature by the main heat exchanger 21 to the lower part of the high-pressure rectification column 23.
  • This high-pressure rectification column (tray or packed column) 23 also requires less than 1/2 the capacity of the gas to be circulated, reducing the capacity to 1/2 or less, and the size is 1 Z 2 or less. .
  • the high-concentration oxygen-containing liquid air 24 of the high-concentration oxygen-containing compressed air Y fed from the supply pipe 22 accumulates at the bottom of the liquid, and the nitrogen gas rises to the top.
  • Part of the nitrogen gas rising to the upper part is introduced into the low-pressure rectification column 28 via the first reflux pipe 31 to the condenser (one condenser) 30 at the bottom, and the remainder is the nitrogen gas extraction pipe 2 It becomes the driving gas for the expansion turbine 37 through 6.
  • the nitrogen gas introduced into the condenser 30 is liquefied there to become liquid nitrogen, and returns to the upper part of the high-pressure rectification column 23 through the second reflux pipe 32 as a reflux liquid.
  • the gas flows downward in the tower 23 and comes into countercurrent contact with the high-concentration oxygen-containing compressed air Y, which rises from below, and the high-boiling component gas (oxygen gas) of the high-concentration oxygen-containing compressed air Y is removed. Liquefied and allowed to flow down.
  • the liquid oxygen-containing liquid air 24 stored at the bottom further becomes oxygen rich, and the low-boiling component gas (nitrogen gas) rises toward the top of the high-pressure rectification column 23.
  • the nitrogen gas extracted from the nitrogen gas extraction pipe 26 is sent to the main heat exchanger 21, and after cooling the compressed air passing through the main heat exchanger 21, passes through the first connection pipe 26 a Then, it is supplied to the expansion tap 37, and as described above, it serves as a driving source of the expansion bin 37 to generate cold.
  • Reference numeral 38 denotes a bypass with an on-off valve 38a.
  • the nitrogen gas introduced into the expansion turbine 37 via the first connection pipe 26a with the nitrogen gas extraction pipe 26 and the on-off valve 26b expands inside to perform thermodynamic external work.
  • the temperature becomes extremely low and the required amount of refrigeration is generated in the device, and in that state, it enters the main heat exchanger 21 via the second connecting pipe 37a, where it exchanges heat with the raw air.
  • the generated cold is given to the raw material air, and the temperature itself becomes normal temperature.Most of the air is discharged as waste gas through the discharge pipe 37b, and part of it is discharged through the branch pipe 40 for the second adsorption. It becomes a regeneration gas for the adsorbent in the towers 12 and 13.
  • the branch pipe 40 functions to supply the introduced nitrogen gas to the first pipe 42 having the heater 41 or the second pipe 43 without a heater.
  • Reference numeral 44 denotes a third pipe which functions to supply the nitrogen gas passed through the first pipe 42 or the second pipe 43 to the first adsorption towers 12 and 13 as adsorbent regeneration gas.
  • Reference numeral 28 denotes a low-pressure rectification tower (shelf-type or packed-column type) provided above the high-pressure rectification tower 23. 24 is sent through a feed pipe 29 with an expansion valve 29a.
  • the low-pressure rectification column 28 is provided with a condenser 30 at the bottom, and a part of the nitrogen gas extracted from the high-pressure rectification column 23 is supplied to the first reflux pipe 31 1 Introduced via Nitrogen gas This, liquid oxygen accumulated in the bottom of the lower pressure rectification column 2 8 (L 0 2:.
  • Purity 9 9 about 7 vol%) 3 4 serve to warming liquid oxygen 3 4 into gas inhibit the And the liquid itself
  • a part of the oxygen is liquefied by the cold heat of the body oxygen 34, and a part of the liquid is returned to the upper part of the high-pressure rectification column 23 through the second reflux pipe 32 with the flow control valve 32a. It becomes a reflux liquid.
  • the remaining liquid nitrogen 34 is introduced into the upper part of the low-pressure rectification tower 28 through a branch pipe 33 with a flow control valve 33 a and becomes a reflux liquid and flows down the low-pressure rectification tower 28. It acts as a gas-liquid separator.
  • Reference numeral 35 denotes a product oxygen gas extraction pipe extending from the lower side of the low-pressure rectification column 28, which is capable of collecting liquid oxygen 34 collected at the bottom of the low-pressure rectification column 28, a high-purity oxygen gas that has been depleted. It is taken out and guided into the main heat exchanger 21 where it exchanges heat with the high-concentration oxygen-containing compressed air Y to bring it to room temperature and send it out as oxygen product gas outside the equipment.
  • Reference numeral 36 denotes a product nitrogen gas extraction pipe extending from the upper part of the low-pressure rectification tower 28, which takes out the nitrogen gas that has risen to the upper part of the low-pressure rectification tower 28 and sends it to the main heat exchanger 21 to have a high concentration.
  • reference numeral 39 denotes a cold box, in which heat insulating material (not shown) such as perlite used for low-temperature heat insulation is packed.
  • heat insulating material such as perlite used for low-temperature heat insulation.
  • the lines of the first adsorption towers 2 and 3 concentrate oxygen by adsorbing nitrogen gas, but use an adsorbent that adsorbs oxygen gas. The removed oxygen gas may be taken out.
  • nitrogen gas and oxygen gas can be produced as follows. That is, first, outside air is taken in from the air compressor (air compression means) 1, where the air is compressed at a low pressure, and the water in the compressed air is removed by a water separator (not shown). in this state fed first adsorption tower (oxygen concentration means) 2, 3, nitrogen gas in the compressed air, 7 minutes, to adsorption removal of carbon dioxide and hydrocarbon gas (C n H m) and the like. Thereby, oxygen gas in the compressed air is concentrated. This is the greatest feature of the present invention.
  • the high-concentration oxygen-containing compressed air X that has passed through the first adsorption towers 2 and 3 is introduced into an oxygen-air compressor (oxygen-air compression means) 11, and the high-concentration oxygen-containing compressed air X is further compressed After the high-concentration oxygen-containing compressed air Y fed to the 2 P ⁇ tower 1 2, 1 3, for adsorbing and removing hyperoxia water containing compressed air Y, carbonated gas and NO x etc. .
  • the high-concentration oxygen-containing compressed air ⁇ ⁇ from which water, carbon dioxide, and ⁇ ⁇ ⁇ have been adsorbed and removed is sent into the main heat exchanger 21 and cooled to an extremely low temperature. Introduce at the bottom of 3.
  • this high-concentration oxygen-containing compressed air Y is brought into countercurrent contact with the reflux liquid produced in the low-pressure rectification column 28 to rectify the compressed air, and the difference between the boiling points of nitrogen and oxygen ( Atmosphere of oxygen I do.
  • This nitrogen gas is taken out from the nitrogen gas extraction pipe 26, sent to the main heat exchanger 21 and then supplied to the expansion turbine 37, where cold is generated, and most of it is discharged outside the device. Part of the gas is used as the regeneration gas for the second adsorption towers 12 and 13.
  • the nitrogen gas collected at the upper part of the low-pressure rectification tower 28 is taken out from the product nitrogen gas extraction pipe 36 and sent to the main heat exchanger 21 where it is heated to near normal temperature and then converted to product nitrogen gas. Send out.
  • liquid oxygen containing high-concentration oxygen which is a liquid stored at the bottom of the high-pressure rectification column 23, is sent to the low-pressure rectification column 28 via the supply pipe 29, and the liquid oxygen from which nitrogen is vaporized and removed. It is stored at the bottom of the low-pressure rectification tower 28 as 3 4 and is vaporized by heat exchange with nitrogen gas passing through the condenser 30 at the bottom of the low-pressure rectification tower 28.
  • the vaporized oxygen gas is taken out of the product oxygen gas extraction pipe 35, sent to the main heat exchanger 21 and heated to near normal temperature, and then sent out of the apparatus as product oxygen gas. And nitrogen gas.
  • the concentration of oxygen gas in the compressed air is reduced to about 20.9 vol.
  • 0 ⁇ 0.50 0) ⁇ Calculated from 0.97, which is about 20, 60 Om 3 / h (No rma 1), which is about 41% of the conventional one described at the beginning. Has decreased.
  • the compression power of the oxygen-air compressor 11 required to produce 100,000 Om 3 / h (No rma 1) oxygen gas is reduced to about 2000 kW, and the oxygen Because it is estimated that the compression power of the air compressor 1 will be about 300 kW, the driving power of the vacuum pump 4 will be about 900 kW, and the electric power of the electric pump 4 will be about 200 kW. 340 kW, which is about 70% of the conventional level. Therefore, energy saving of 30% or more can be realized.
  • First adsorption towers 2 and 3 for concentrating oxygen gas in the compressed air are provided to increase the oxygen concentration in the raw material air, which is passed through the oxygen-air compressor 11 and the main heat exchanger 21 to high-pressure purification.
  • Distillation tower 23, low-pressure rectification tower 28 Therefore, by realizing a drastic reduction in the flow rate of each device such as the main heat exchanger 21 and the two rectification columns 23 and 28 after the oxygen-air compressor 11, The size of the device can be reduced to less than half, and as a result, the entire device can be significantly reduced in size.
  • the diameter of the high-pressure rectification column 23 is 7 m (calculated by our company) with the conventional one, which is It was necessary to assemble on-site because there was no transportation means to assemble and transport it to the site, but in this embodiment, when producing the same amount of oxygen, the gas flowing through the rectification column Is less than 1/2, the diameter of the rectification column can be reduced to about 4.2 m. As a result, it is possible to assemble the products at the factory and transport them to the site, which can save a great deal of labor.
  • FIG. 2 shows another embodiment of the air separation device of the present invention.
  • the second adsorption towers 12 and 13 are omitted. That is, the second adsorption towers 12 and 13, the second discharge pipe 14, the on-off valves 16a, 16b, 17a, 17b, 18a, 18b; 19a, 1
  • the pipe line with 9b, the branch pipe 40 and the first to third pipes 42 to 44 are omitted.
  • Other parts are the same as those in the above embodiment, and the same parts are denoted by the same reference numerals.
  • the device by installing the device in a place where clean air is used as raw material air, the same effects as in the above embodiment can be obtained, and the device can be simplified and downsized. .
  • FIG. 3 shows still another embodiment of the air separation device of the present invention.
  • a liquid oxygen storage tank (not shown) in which liquid oxygen (L0 2 ) is supplied from outside the apparatus by a tank opening or the like.
  • the apparatus is substantially the same as the apparatus shown in FIG. 2, except that the liquid oxygen is used as a cold source.
  • reference numeral 47 denotes an introduction pipe for introducing the liquid oxygen from the liquid oxygen storage tank to the lower part of the low-pressure rectification column 28 as a cold source. It flows down to the bottom of the rectification column 28 and joins the liquid oxygen 34 collected at this bottom.
  • the supercooler 49 is provided with high-concentration oxygen-containing liquid air 24 in the supply pipe 29, liquid nitrogen (reflux liquid) in the branch pipe 33, and products in the nitrogen gas extraction pipe 36.
  • the high-concentration oxygen-containing liquid air 24 in the supply pipe 29 is cooled by passing the product nitrogen gas and the waste nitrogen gas in the discharge pipe 48.
  • Reference numeral 50 denotes a liquid oxygen extraction pipe extending from the bottom of the low-pressure rectification tower 28, which takes out the liquid oxygen collected at the bottom of the low-pressure rectification tower 28 and guides it into the main heat exchanger 21 to produce high-concentration oxygen. While cooling the contained compressed air Y, it acts to raise itself to room temperature and introduce it into the product oxygen gas extraction pipe 35 as product oxygen gas.
  • Reference numeral 51 denotes a product nitrogen gas compressor provided in the product nitrogen gas extraction pipe 36, which acts to increase the product nitrogen gas passing through the product nitrogen gas extraction pipe 36 to a predetermined pressure.
  • Reference numeral 2 denotes a first product oxygen gas compressor provided in the product oxygen gas extraction pipe 35, and the product oxygen gas passing through the product oxygen gas extraction pipe 35 is pressurized to a predetermined pressure to obtain a low-pressure product oxygen gas extraction pipe. It acts to supply 5 3.
  • 5 4 is a second oxygen product gas compressor, first, to the effect supplied to the high pressure product oxygen gas takeout pipe 5 5 further boost the product oxygen gas through the oxygen product gas compressor 5 2.
  • the ceiling surface of 23 and the bottom surface of the low-pressure rectification tower 28 provided above the high-pressure rectification tower 23 are integrated and formed of the same material.
  • 36a is the product nitrogen gas extraction pipe
  • 39 A is a cold box, which is filled with a heat insulating material such as pearlite and has a vacuum suction.
  • Other parts are the same as those of the embodiment shown in FIG. 2, and the same parts are denoted by the same reference numerals.
  • nitrogen gas and oxygen gas can be produced as follows. That is, in the same manner as in the embodiment shown in FIG. 2, external air is taken in from an air compressor (air compression means) 1, where the air is compressed at a low pressure and compressed by a zK separator (not shown). The moisture in the compressed air is removed and sent to the first adsorption tower (oxygen concentrating means) 2 and 3 in that state, and the nitrogen gas, moisture, carbon dioxide gas and carbonized gas in the compressed air are removed. Hydrogen gas (C n H m) and the like are adsorbed and removed. This enriches the oxygen gas in the compressed air.
  • the high-concentration oxygen-containing compressed air X that has passed through the first P and the landing towers 2 and 3 is introduced into an oxygen-air compressor (oxygen-air compression means) 11, and the oxygen-air compressor 11 generates high-concentration oxygen-containing air.
  • Compressed air X is further compressed to obtain high-concentration oxygen-containing compressed air Y.
  • the high-concentration oxygen-containing compressed air Y is sent into the main heat exchanger 21 to be cooled to an extremely low temperature, and then introduced into the lower part of the high-pressure rectification column 23 in that state.
  • the high-concentration oxygen-containing compressed air Y and the reflux liquid produced in the low-pressure rectification column 28 are brought into countercurrent contact to rectify the compressed air, thereby obtaining nitrogen and oxygen.
  • Liquefaction of oxygen which is a high-boiling component in high-concentration oxygen-containing compressed air Y, due to the difference in boiling point of oxygen (boiling point of oxygen at atmospheric pressure-18 ° C, also boiling point of nitrogen-196 ° C) To make nitrogen gas.
  • the nitrogen gas collected at the top of the low-pressure rectification column 28 is taken out from the product nitrogen gas extraction pipe 36, sent to the supercooler (heat exchanger) 49, and introduced into the main heat exchanger 21. After the temperature is raised to near normal temperature in the heat exchanger 21, it is sent out of the equipment as product nitrogen gas.
  • the high-concentration oxygen-containing liquid air 24 collected at the bottom of the high-pressure rectification column 23 is sent to the supercooler 49 via the supply pipe 29, where the high-concentration oxygen containing the cooled gas-liquid mixture is contained.
  • the liquid air 24 is sent to the low-pressure rectification tower 28, and the nitrogen is vaporized and removed.
  • the liquid oxygen 34 is stored at the bottom of the low-pressure rectification tower 28, and the nitrogen passes through the condenser 30 at the bottom of the low-pressure rectification tower 28. It is vaporized by heat exchange with gas.
  • the vaporized oxygen gas is taken out from the product oxygen gas extraction pipe 35, sent to the main heat exchanger 21 and heated to near normal temperature, and then the product oxygen gas passed through the first product oxygen compressor 52 is reduced in pressure.
  • the product oxygen gas is sent out of the device by the product oxygen gas extraction pipe 53, and the product oxygen gas that has passed through the second product oxygen compressor 54 is sent out of the device by the high-pressure product oxygen gas extraction pipe 55. In this way, product oxygen gas and nitrogen gas are obtained.
  • FIG. 4 shows still another embodiment of the air separation device of the present invention.
  • a liquid nitrogen storage tank (not shown) in which liquid nitrogen (LN 2 ) is supplied from outside the apparatus by a tank trolley or the like instead of the expansion bottle 37 Except that the liquid nitrogen is used as the cold source.
  • 47a is an introduction pipe for introducing the liquid nitrogen from the liquid nitrogen storage tank into the upper part of the high-pressure rectification column 23 as a cold source.
  • Part of the liquid nitrogen liquefied in the condenser 30 at the lower part of the low-pressure rectification tower 28 is introduced into the upper part of the high-pressure rectification tower 23.
  • Other parts are the same as those of the embodiment shown in FIG. 2, and the same parts are denoted by the same reference numerals.
  • FIG. 5 shows still another embodiment of the air separation device of the present invention.
  • a first feed pipe 1a for feeding compressed air passed through an air compressor 1 to first adsorption towers 2 and 3;
  • the introduction pipe 57 for introducing the highly concentrated oxygen-containing compressed air X passed through 3 into the oxygen-air compressor 11 (not denoted by 57 in FIG. 1) is connected to an on-off valve (or a flow control valve).
  • an on-off valve or a flow control valve
  • Communication pipe 58 communicates. Then, the on-off valve 58a is opened, and a part of the compressed air that has passed through the air compressor 1 and the water separator (not shown) is directly passed through the communication pipe 58 (that is, the first adsorbent).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
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  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
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  • Separation By Low-Temperature Treatments (AREA)
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  • Drying Of Gases (AREA)

Abstract

An air separator with which oxygen gas can be produced in an energy-saving manner and that enables a device to be remarkably downsized. The air separator has an air compressor (1) for taking in air from the outside and compressing it, first adsorption columns (2, 3) for condensing oxygen gas that is contained in the air compressed by the air compressor (1), an oxygen/air compressor (11) for further compressing high-density oxygen gas-containing compressed air (X) came through the first adsorption columns (2, 3), a main heat exchanger (21) for cooling a high-density oxygen-containing compressed air (Y) came through the oxygen/air compressor (11), and high-pressure rectification column (23) and a low-pressure rectification column (28) that are used for taking out oxygen gas by decomposing, using differences in boiling points of component gases, the high-density oxygen-containing compressed air (Y) having been cooled to a lower temperature through the main heat exchanger (21).

Description

明細: 空気分離装置 技術分野  Description: Air separation unit Technical field

本発明は、 酸素ガスを省エネルギーで製造することができ、 装置を著しく小形 化できる空気分離装置に関するものである。 背景技術  TECHNICAL FIELD The present invention relates to an air separation device that can produce oxygen gas with energy saving and that can significantly reduce the size of the device. Background art

一般に、 窒素ガス （GN2 ) , 酸素ガス （G〇2 ) , アルゴン （Ar) 等は、 図 6に示すように、 空気を原料とし、 これを空気圧縮機 6 1で圧縮したのち、 吸 着塔 6 2に入れて圧縮空気中の水 (Η2 0) ， 炭酸ガス (C〇2 ) および炭化水 素ガス (Cn Mm ) を吸着除去し、 さらに、 コールドボックス 63内の主熱交換 器 （図示せず） を通して冷媒と熱交換させて超低温に冷却し、 つぎに、 精留塔 （ 図示せず) 内で深冷分離して製品ガス (窒素ガス， 酸素ガス等） を製造し、 これ を上記主熱交換器を通して常温近くまで昇温させるという工程を経て製造されて いる。 また、 コールドボックス 63から取り出される廃ガスは、 吸着塔 6 の再 生用として利用されている （例えば、 特開平 8— 26 1 644号公報を参照） 。 図 6において、 64は再生 ·排気用のヒータ一である。 Generally, as shown in FIG. 6, nitrogen gas (GN 2 ), oxygen gas (G （ 2 ), argon (Ar), etc. are obtained by using air as a raw material, compressing it with an air compressor 61, and adsorbing it. water compressed air placed in the tower 6 2 (Eta 2 0), carbon dioxide (C_〇 2) and hydrocarbons gas (C n M m) to adsorb and remove further main heat exchanger in the cold box 63 Heat exchange with the refrigerant through a vessel (not shown) to cool it to ultra-low temperature, and then cryogenically separate in a rectification tower (not shown) to produce product gas (nitrogen gas, oxygen gas, etc.) It is manufactured through a process of raising the temperature to near normal temperature through the main heat exchanger. The waste gas extracted from the cold box 63 is used for regeneration of the adsorption tower 6 (see, for example, Japanese Patent Application Laid-Open No. 8-261644). In FIG. 6, reference numeral 64 denotes a heater for regeneration and exhaust.

このような空気分離装置では、 空気圧縮機 6 1として、 通常、 吐出圧力が 5 k g/cm2 G CO. 5MPaG (ゲージ圧） 〕 程度の空気圧縮機 6 1が使用され ているが、 この空気圧縮機 6 1を用いて 1 0， 000 m3 /h (No rma 1 ) の酸素ガスを製造しょうとすると、 これに必要な空気量は、 空気の各成分ガスの 成分割合 (体積0 /0) が、 酸素 2 0 · 9 %：窒素 78. 1 %：アルゴン 0. 9 %で あるため、 酸素ガスの回収効率を 97%とすると、 理論上では、 空気量 = ( 1 0 ， 000 + 0. 209 ) ÷0. 97で算出され、 約 50 , 000 m3 /h (N o rma 1 ) の空気量が必要となる。 このため、 上記必要な空気量に見合う吸着塔 62, 主熱交換器， 精留塔等を使用する必要があり、 装置全体が大掛かりになつ ている。 しかも、 1 0, 000 m3 /h (No rma 1 ) の酸素ガスを製造する 場合、 これに必要な空気圧縮機 6 1の圧縮動力 （この圧縮動力は、 通常、上記必 要な空気量の数値に約 0 . 0 9を乗じた値とされている） 力 5 0 0 k W程度で ありヽ 吸着塔 6 2の再生 ·排気用のヒーター 6 4の駆動動力が 5 0 0 k W程度で あるため、 合計 5 0 0 0 k W程度の大きな動力を必要とし、 酸素ガスの製造に多 大なエネルギーを要している。 In such an air separation device, an air compressor 61 having a discharge pressure of about 5 kg / cm 2 G CO. 5 MPag (gauge pressure) is usually used as the air compressor 61. When using a compressor 6 1 and you'll produce 1 0, the oxygen gas 000 m 3 / h (No rma 1), amount of air required for this, the component ratio of each component gas of air (volume 0/0 ) Is 20.9% oxygen: 78.1% nitrogen: 0.9% argon. If the oxygen gas recovery efficiency is 97%, then, in theory, the air volume = (10,000 + 0) 209) 算出 Calculated from 0.97, requiring an air volume of about 50,000 m 3 / h (Norma 1). For this reason, it is necessary to use an adsorption tower 62, a main heat exchanger, a rectification tower, and the like corresponding to the required air amount, and the entire apparatus becomes large-scale. Moreover, it produces oxygen gas of 10,000 m 3 / h (No rma 1). In this case, the necessary compression power of the air compressor 61 (this compression power is usually a value obtained by multiplying the above required air amount by about 0.09) Power 500 k The power of the heater 64 for regeneration and exhaust of the adsorption tower 62 is about 500 kW, so a large power of about 500 kW is required, It requires a lot of energy for manufacturing.

本発明は、 このような事情に鑑みなされたもので、酸素ガスを省エネルギーで 製造することができ、深冷分離機構 （コールドボックスおよびその内部機器） 等 を大幅に小形化できる空気分離装置の提供をその目的とする。 発明の開示  The present invention has been made in view of such circumstances, and provides an air separation device that can produce oxygen gas with energy saving and that can greatly reduce the size of a cryogenic separation mechanism (a cold box and its internal equipment). For that purpose. Disclosure of the invention

上記の目的を達成するため、本発明の空気分離装置は、外部より空気を取り入 れて低圧で圧縮する空気圧縮手段と、 この空気圧縮手段によつて圧縮された圧縮 空気中の酸素ガスを濃縮する酸素濃縮手段と、 この酸素濃縮手段を経た高濃度酸 素含有圧縮空気 Xをさらに圧縮する酸素空気圧縮手段と、 この酸素空気圧縮手段 を経た高濃度酸素含有圧縮空気 Yを冷却する熱交換器と、 この熱交換器を経由し 低温に冷却された高濃度酸素含有圧縮空気 Yを各成分ガスの沸点差を利用して分 離し酸素ガスを取り出す精留塔とを備えたという構成をとる。  In order to achieve the above object, an air separation device of the present invention includes an air compression unit that takes in air from the outside and compresses it at a low pressure, and enriches oxygen gas in compressed air compressed by the air compression unit. Oxygen condensing means, oxygen-air compression means for further compressing the high-concentration oxygen-containing compressed air X passed through the oxygen concentrating means, and heat exchanger for cooling the high-concentration oxygen-containing compressed air Y passed through the oxygen-air compression means And a rectification column for separating the high-concentration oxygen-containing compressed air Y cooled to a low temperature via the heat exchanger by utilizing the boiling point difference of each component gas to take out the oxygen gas.

すなわち、本発明の空気分離装置は、 空気圧縮手段により原料空気を低圧力に 圧縮し、 この空気圧縮手段に続いて、 その圧縮空気中の酸素ガスを濃縮する酸素 濃縮手段を設け、 原料空気中の酸素濃度を高め、 これを、 酸素空気圧縮手段， 熱 交換器を経由して精留塔に供給している。 そのため、 同一量の酸素ガス等を製造 する場合、 大幅なエネルギーの節約ができるとともに、 酸素濃縮手段以降の各手 段の流通流量の大幅な低減を実現することにより、 それらを従来のものの半分以 下に小形ィ匕でき、 結果的に装置全体の著しい小形化を達成することができる。 こ こで、上記低圧とは、 酸素空気圧縮手段による圧縮圧力よりも小さいことをいい 、 通常は、 酸素空気圧縮手段の圧縮圧力の 1 / 3以下、好適には 1 / 5以下、 よ り好適には 1 / 1 0以下のことをいう。  That is, the air separation device of the present invention compresses the raw material air to a low pressure by the air compressing means, and provides the oxygen condensing means for concentrating the oxygen gas in the compressed air following the air compressing means. The oxygen concentration is increased, and this is supplied to the rectification column via oxygen-air compression means and a heat exchanger. Therefore, when producing the same amount of oxygen gas, etc., it is possible to save a large amount of energy and realize a significant reduction in the flow rate of each means after the oxygen enrichment means, thereby reducing them to more than half that of the conventional method. The device can be downsized, and consequently the entire device can be significantly reduced in size. Here, the low pressure refers to a pressure lower than the compression pressure of the oxygen-air compression means, and is usually 1/3 or less, preferably 1/5 or less, more preferably 1/3 of the compression pressure of the oxygen-air compression means. Means less than 1/10.

また、上記酸素濃縮手段を、 圧縮空気中の窒素ガスを吸着する吸着剤を収容す る吸着塔とし、上記吸着剤で圧縮空気中の水分等の不純物をも除去するようにし た場合には、上記吸着塔の吸着剤の作用により圧縮空気中の酸素ガスを濃縮させ ることができるうえ、圧縮空気中の水分をも除去できるため、酸素濃縮手段に続 く酸素空気圧縮手段で圧縮する対象は、 より乾燥したものとなり、 圧縮動力をよ り減少させることができる。 Further, the oxygen concentrating means is an adsorption tower containing an adsorbent for adsorbing nitrogen gas in the compressed air, and the adsorbent removes impurities such as moisture in the compressed air. In this case, the oxygen gas in the compressed air can be concentrated by the action of the adsorbent of the adsorption tower and the moisture in the compressed air can also be removed. The object to be compressed with is dried and the compression power can be further reduced.

また、 酸素空気圧縮手段と熱交換器との間に、 高濃度酸素含有圧縮空気 Y中の 不純物を除去する除去手段を設けたときは、上記高濃度酸素含有圧縮空気 Y中に 、微量残存する炭化水素， 分， Ν Ο χ等を除去することができ、 原料空気とし て海岸沿いの空気 (ナトリウムイオン多い) または道路沿いの空気 （自動車排ガ ス多い） 等、 黉の悪い空気も利用できるようになる。  Further, when a removing means for removing impurities in the high-concentration oxygen-containing compressed air Y is provided between the oxygen-air compression means and the heat exchanger, a trace amount remains in the high-concentration oxygen-containing compressed air Y. It can remove hydrocarbons, minerals, Ν Ο χ, etc., and can use poor air such as air along the coast (a lot of sodium ions) or air along the road (a lot of exhaust gas from automobiles) as raw material air. Become like

また、 酸素濃縮手段を経た高濃度酸素含有圧縮空気 Xを酸素空気圧縮手段に導 入する導入路に、 空気圧縮手段によって圧縮された圧縮空気の一部を、酸素濃縮 手段を経由させることなく、 直接供給するようにした場合には、 空気圧縮手段を 経たのち上記導入路に直接供給される圧縮空気の一部と、 空気圧縮手段を経たの ち酸素濃縮手段に導入されここで高濃度酸素含有圧縮空気 Xとなつて上記導入路 に供給される圧縮空気の残部とを、上記導入路で合流させ、 これにより、 高濃度 酸素含有圧縮空気 X中の酸素濃度を薄めることができるため、酸素製造量を少な くしたいときには、上記導入路に直接供給する圧縮空気量を調整することで、 対 応することができるようになる。 図面の簡単な説明  In addition, a part of the compressed air compressed by the air compression means is introduced into the introduction path for introducing the high-concentration oxygen-containing compressed air X having passed through the oxygen concentration means to the oxygen-air compression means without passing through the oxygen concentration means. In the case of supplying directly, a part of the compressed air which is directly supplied to the above-mentioned introduction path after passing through the air compressing means, and is introduced into the oxygen concentrating means after passing through the air compressing means and contains high-concentration oxygen. The remaining portion of the compressed air supplied to the introduction path as the compressed air X is merged in the introduction path, whereby the oxygen concentration in the high-concentration oxygen-containing compressed air X can be reduced. When it is desired to reduce the amount, the amount of compressed air supplied directly to the above-mentioned introduction passage can be adjusted to cope with it. BRIEF DESCRIPTION OF THE FIGURES

第 1図は、本発明の空気分離装置の一実施の形態を示す構成図であり、第 2図は 、 本発明の空気分離装置の他の実施の形態を示す構成図であり、 第 3図は、 本発 明の空気分離装置のさらに他の実施の形態を示す構成図であり、 第 4図は、 本発 明の空気分離装置のさらに他の実施の形態を示す構成図であり、 第 5図は、 本発 明の空気分離装置のさらに他の実施の形態を示す構成図であり、 第 6図は、 従来 例を示す構成図である。 発明を実施するための最良の形態 FIG. 1 is a configuration diagram showing one embodiment of the air separation device of the present invention, and FIG. 2 is a configuration diagram showing another embodiment of the air separation device of the present invention. Fig. 4 is a configuration diagram showing still another embodiment of the air separation device of the present invention; Fig. 4 is a configuration diagram showing still another embodiment of the air separation device of the present invention; FIG. 5 is a configuration diagram showing still another embodiment of the air separation device of the present invention, and FIG. 6 is a configuration diagram showing a conventional example. BEST MODE FOR CARRYING OUT THE INVENTION

図 1は本発明の空気分離装置の一実施の形態を示している。 図において、 1は 大気を取り込んで圧縮する空気圧縮機 （空気圧縮手段） であり、 その吐出圧力はFIG. 1 shows an embodiment of the air separation device of the present invention. In the figure, 1 is It is an air compressor (air compression means) that takes in the air and compresses it.

、 0. 1 kg/cm2 G CO. 0 IMP aG (ゲージ圧） 〕 程度の低圧に設定さ れている。 1 aは空気圧縮機 1を経た圧縮空気を第 1 P及着塔 2 , 3に送給する第 1送給パイプである。 第 1吸着塔 （酸素濃縮手段） 2, 3は、 内部に、 上流側が シリ力ゲル等の吸着剤が充塡され、 下流側に当出願人が開発したモレキュラーシ —ブス製吸着剤 （エア ·ウォー夕一社製 AW 02 03 ) 力充塡されている。 この 第 1吸着塔 2, 3は、 2個一対となっていて吸着'再生を交互に切換え運転する 。 この実施の形態では、第 1吸着塔 2， 3の吸着剤の作用 （窒素ガス吸着作用） により、 空気圧縮機 1を経た低圧の圧縮空気中の各成分ガスの成分割合 （体積％ ) を、 例えば、酸素ガス 50% :窒素ガス 47. 5 %：アルゴンガス 2. 5 %程 度にし、 圧縮空気中の酸素ガスの濃度を 20. 9体積％から 50体積％に濃縮し ている。 第 1吸着塔 2， 3は、上記の濃縮と同時に吸着剤の作用により圧縮空気 中の水 (H2 0) ， 炭酸ガス (C02 ) および炭化水素ガス (C„ Hm ) 等を吸 着除去する。 4は第 1吸着塔 2, 3の再生 ·排気用の真空ポンプであり、 4 aは 第 1放出パイプで、 第 1吸着塔 2 , 3の吸着剤に吸着された廃ガスを大気に放出 し吸着剤を再生する作用をする。 このように、第 1吸着塔 2， 3およびその開閉 弁 6 a, 6 b, 8 a, 8 b付きのパイプ路ならびに真空ポンプ 4からなる系は、 VS A (バキュームスイングアブソープド） 、膜分離となっていて一方の第 1吸 着塔 2 (3) が吸着作動しているときは、 他方の第 1吸着塔 3 (2) は真空ボン プ 4の真空吸引により再生されている。 なお、上記空気圧縮機 1と第 1吸着塔 2 ， 3との間には、 空気圧縮機 1により圧縮された圧縮空気中の水分を除去する水 分離器 （図示せず） 、 場合により、 この水分離器を経た圧縮空気を冷却するフロ ン冷却器 （図示せず） が設けられていてる。 また、 この実施の形態では、上記の 系は VS Aとなっているが、 PSA (プレッシャースイングアブソープド) ， T, 0.1 kg / cm 2 G CO. 0 IMP aG (gauge pressure)]. Reference numeral 1a denotes a first feed pipe for feeding the compressed air that has passed through the air compressor 1 to the first P connecting towers 2 and 3. The first adsorption tower (oxygen concentrating means) 2 and 3 has an upstream side filled with an adsorbent such as silica gel on the upstream side, and a molecular sieve adsorbent (air / air) developed by the applicant on the downstream side. AW 02 03 manufactured by War Yuichisha. The first adsorption towers 2 and 3 are paired and operated by alternately switching between adsorption and regeneration. In this embodiment, by the action of the adsorbent of the first adsorption towers 2 and 3 (nitrogen gas adsorption action), the component ratio (volume%) of each component gas in the low-pressure compressed air passed through the air compressor 1 is calculated as follows. For example, oxygen gas 50%: nitrogen gas 47.5%: argon gas is about 2.5%, and the concentration of oxygen gas in compressed air is increased from 20.9% by volume to 50% by volume. First adsorption tower 2, 3, water (H 2 0) in the compressed air by the action of the above-mentioned concentration at the same time the adsorbent, carbon dioxide (C0 2) and hydrocarbon gas (C "H m) adsorption, etc. Reference numeral 4 denotes a vacuum pump for regenerating and exhausting the first adsorption towers 2 and 3, and reference numeral 4a denotes a first discharge pipe for removing waste gas adsorbed by the adsorbents of the first adsorption towers 2 and 3 to the atmosphere. Thus, the system consisting of the first adsorption towers 2, 3 and the pipe lines with the on-off valves 6a, 6b, 8a, 8b and the vacuum pump 4 is constructed as follows. , VS A (vacuum swing absolute), membrane separation, and when one of the first adsorption towers 2 (3) is performing adsorption operation, the other first adsorption tower 3 (2) is vacuum pumped. It is regenerated by the vacuum suction of the pump 4. Between the air compressor 1 and the first adsorption towers 2 and 3, moisture in the compressed air compressed by the air compressor 1 is removed. A water separator (not shown) is provided for cooling the compressed air that has passed through the water separator, if necessary. Is VS A, but PSA (Pressure Swing Absorbed), T

5 A (サ一マルスイングアブソープド).の膜分離であってもよい。 図において、It may be a membrane separation of 5 A (summarized swing absorbed). In the figure,

6 a, 6 b, 7 a, 7 b, 8 a, 8 bは第 1吸着塔 2 , 3を交互に吸着.再生運 転させるための開閉弁である。 Reference numerals 6a, 6b, 7a, 7b, 8a, and 8b denote on-off valves for alternately adsorbing and regenerating the first adsorption towers 2 and 3.

1 1は第 1吸着塔 2， 3を経た高濃度酸素含有圧縮空気 Xをさらに圧縮する小 形の酸素空気圧縮機 （流通する気体が従来のものの 1 Z 2以下になるため、 1 / 2以下の小形サイズで足りる） 〔酸素空気圧縮手段〕 である。 この実施の形態で は、上記酸素空気圧縮機 1 1として、 高濃度酸素含有圧縮空気 Xをさらに圧縮す る小形の酸素空気圧縮機 （オイルレスのセントリフユ一ガルコンプレッサー：吐 出圧力 5 kg/cm2 G 〔0. 5MP aG (ゲージ圧） 〕 程度の酸素空気圧縮機 ) が用いられている。 この酸素空気圧縮機 11は、 高濃度酸素含有圧縮空気 Xを さらに圧縮する際の爆発を防ぐため、 オイルレス等の機構となっている。 1 1 a は酸素空気圧縮機 1 1を経た高濃度酸素含有圧縮空気 Yを第 2吸着塔 12, 13 に送気する第 2送給パイプである。 12, 13は内部に、市販モレキュラーシ一 ブス等の吸着剤が充塡され、 交互に吸着 ·再生を行う 2個 1組の小形の第 2吸着 塔 (従来のものの 1 / 2以下の小形のサイズになつている) であり、酸素空気圧 縮機 1 1によりさらに圧縮された高濃度酸素含有圧縮空気 Y中に微量残存する水 ， 炭酸ガス， Cn Mraおよび NOx等を吸着除去する作用をする。 1 4は第 2放 出パイプで、第 2吸着塔 12, 1 3で再生作用を終えた廃ガスを大気に放出する 作用をする。 この第 2吸着塔 12, 1 3および開閉弁 1 6 a, 1 6 b, 1 9 a, 1 9 b付きのパイプ路からなる系は、 TS Aとなっている。 図において、 1 6 a , 1 6 b, 1 7 a, 1 7 b, 18 a, 18 b, 1 9 as 19 bは第 2吸着塔 12 ， 1 3を交互に吸着'再生運転させるための開閉弁である。 1 1 is a small oxygen-air compressor that further compresses the high-concentration oxygen-containing compressed air X that has passed through the first adsorption towers 2 and 3. (A small size of 2 or less is sufficient.) [Oxygen-air compression means]. In this embodiment, the oxygen-air compressor 11 is a small-sized oxygen-air compressor (oil-less centrifugal compressor: discharge pressure 5 kg / cm2) that further compresses the high-concentration oxygen-containing compressed air X. An oxygen air compressor of about 2 G [0.5MPaG (gauge pressure)] is used. The oxygen-air compressor 11 has an oil-less mechanism or the like in order to prevent explosion when compressing the high-concentration oxygen-containing compressed air X further. Reference numeral 11a denotes a second supply pipe for supplying the high-concentration oxygen-containing compressed air Y having passed through the oxygen-air compressor 11 to the second adsorption towers 12, 13. 12 and 13 are filled with an adsorbent such as a commercially available molecular sieve, and alternately adsorb and regenerate.A set of two small second adsorption towers (smaller than the conventional ones) a summer in which) the size, action for adsorbing and removing water traces remaining on hyperoxia-containing compressed air Y which further compressed by the oxygen pressure compressor 1 1, carbon dioxide, a C n M ra and NO x, etc. do. Reference numeral 14 denotes a second discharge pipe, which discharges waste gas that has been regenerated in the second adsorption towers 12, 13 to the atmosphere. The system including the pipe lines with the second adsorption towers 12, 13 and the on-off valves 16a, 16b, 19a, 19b is TSA. In FIG, 1 6 a, 1 6 b , 1 7 a, 1 7 b, 18 a, 18 b, 1 9 a s 19 b is for adsorbing 'regeneration operation alternately second adsorption tower 12, 1 3 It is an on-off valve.

2 1は主熱交換器で、 プレートフィン型のもの等からなり、第 2吸着塔 12， 1 3により、 微量の水および炭酸ガス等が吸着除去された高濃度酸素含有圧縮空 気 Yを超低温に冷却する。 この主熱交換器 2 1も、 従来のものの 1/2の流通気 体の処理量となることから、約 1/2以下の小形のサイズになる。 22は主熱交 換器 2 1により超低温に冷却された高濃度酸素含有圧縮空気 Yを高圧精留塔 23 の下部に送り込む供給パイプである。 この高圧精留塔 (棚段式またはパックドカ ラム式) 23も、 流通する気体が従来の 1/2以下になることから、 1/2以下 の能力でよくなり、 1 Z 2以下のサイズになる。 上記高圧精留塔 23の内部では 、供給パイプ 22から送り込まれた高濃度酸素含有圧縮空気 Yのうち、 液体の高 濃度酸素含有液体空気 24力底部に溜まり、 窒素ガスが上部に上昇する。 上部に 上昇する窒素ガスは、 その一部が第 1還流用パイプ 31を経由して低圧精留塔 2 8下部の凝縮器 （コンデンサ一） 30に導入され、 残部が窒素ガス取出パイプ 2 6を経由し膨脹タービン 3 7の駆動ガスとなる。 そして、 凝縮器 3 0に導入され た窒素ガスは、 そこで液ィ匕されて液体窒素となり、 第 2還流用パイプ 3 2を経て 高圧精留塔 2 3の上部に還流液として戻り、 高圧精留塔 2 3内を下方に流下し、 下方から上昇してくる気体の高濃度酸素含有圧縮空気 Yと向流的 接触し、 高濃 度酸素含有圧縮空気 Yの高沸点成分ガス （酸素ガス） を液化し流下させる。 この ため、 底部に溜まる液体の高濃度酸素含有液体空気 2 4はさらに酸素リツチにな り、 低沸点成分ガス （窒素ガス） は高圧精留塔 2 3の上部に向かって上昇する。 窒素ガス取出パイプ 2 6から取出された窒素ガスは、 主熱交換器 2 1に送られ、 この主熱交換器 2 1を通過する圧縮空気を冷却したのち、 第 1連結パイプ 2 6 a を経由して膨脹タ一ピ、ン 3 7に供給され、 先に述べたように、 膨脹夕一ビン 3 7 の駆動源となり寒冷を発生する。 3 8は開閉弁 3 8 a付き迂回路である。 すなわ ち、 窒素ガス取出パイプ 2 6 , 開閉弁 2 6 b付き第 1連結パイプ 2 6 aを経て膨 脹タービン 3 7に導入された窒素ガスは、 内部で膨脹し、 熱力学的外部仕事を行 うことにより著しく低温になつて装置に必要な寒冷量を発生し、 その状態で第 2 連結パイプ 3 7 aを経由して主熱交換器 2 1に入り、 ここで原料空気と熱交換し て発生寒冷を原料空気に付与し、 それ自身は常温となり、 その大部分は、 廃ガス として放出パイプ 3 7 bを経由して放出され、 一部が分岐パイプ 4 0を経由して 第 2吸着塔 1 2， 1 3の吸着剤の再生ガスとなる。 この分岐パイプ 4 0は、 導入 された窒素ガスを、 ヒー夕 4 1を有する第 1パイプ 4 2もしくは、 ヒータなしの 第 2パイプ 4 3に供給する作用をする。 4 4は第 3パイプであり、 第 1パイプ 4 2もしくは第 2パイプ 4 3を経た窒素ガスを第 吸着塔 1 2 , 1 3に吸着剤再生 用ガスとして供給する作用をする。 21 is a main heat exchanger composed of a plate-fin type, etc., and uses the second adsorption towers 12, 13 to convert the high-concentration oxygen-containing compressed air Y from which trace amounts of water and carbon dioxide have been adsorbed and removed to an ultra-low temperature. Cool. Since the main heat exchanger 21 also has a throughput of half of the flow rate of the conventional one, it has a small size of about 1/2 or less. Reference numeral 22 denotes a supply pipe for sending the high-concentration oxygen-containing compressed air Y cooled to an extremely low temperature by the main heat exchanger 21 to the lower part of the high-pressure rectification column 23. This high-pressure rectification column (tray or packed column) 23 also requires less than 1/2 the capacity of the gas to be circulated, reducing the capacity to 1/2 or less, and the size is 1 Z 2 or less. . Inside the high-pressure rectification column 23, the high-concentration oxygen-containing liquid air 24 of the high-concentration oxygen-containing compressed air Y fed from the supply pipe 22 accumulates at the bottom of the liquid, and the nitrogen gas rises to the top. Part of the nitrogen gas rising to the upper part is introduced into the low-pressure rectification column 28 via the first reflux pipe 31 to the condenser (one condenser) 30 at the bottom, and the remainder is the nitrogen gas extraction pipe 2 It becomes the driving gas for the expansion turbine 37 through 6. Then, the nitrogen gas introduced into the condenser 30 is liquefied there to become liquid nitrogen, and returns to the upper part of the high-pressure rectification column 23 through the second reflux pipe 32 as a reflux liquid. The gas flows downward in the tower 23 and comes into countercurrent contact with the high-concentration oxygen-containing compressed air Y, which rises from below, and the high-boiling component gas (oxygen gas) of the high-concentration oxygen-containing compressed air Y is removed. Liquefied and allowed to flow down. As a result, the liquid oxygen-containing liquid air 24 stored at the bottom further becomes oxygen rich, and the low-boiling component gas (nitrogen gas) rises toward the top of the high-pressure rectification column 23. The nitrogen gas extracted from the nitrogen gas extraction pipe 26 is sent to the main heat exchanger 21, and after cooling the compressed air passing through the main heat exchanger 21, passes through the first connection pipe 26 a Then, it is supplied to the expansion tap 37, and as described above, it serves as a driving source of the expansion bin 37 to generate cold. Reference numeral 38 denotes a bypass with an on-off valve 38a. In other words, the nitrogen gas introduced into the expansion turbine 37 via the first connection pipe 26a with the nitrogen gas extraction pipe 26 and the on-off valve 26b expands inside to perform thermodynamic external work. As a result, the temperature becomes extremely low and the required amount of refrigeration is generated in the device, and in that state, it enters the main heat exchanger 21 via the second connecting pipe 37a, where it exchanges heat with the raw air. The generated cold is given to the raw material air, and the temperature itself becomes normal temperature.Most of the air is discharged as waste gas through the discharge pipe 37b, and part of it is discharged through the branch pipe 40 for the second adsorption. It becomes a regeneration gas for the adsorbent in the towers 12 and 13. The branch pipe 40 functions to supply the introduced nitrogen gas to the first pipe 42 having the heater 41 or the second pipe 43 without a heater. Reference numeral 44 denotes a third pipe which functions to supply the nitrogen gas passed through the first pipe 42 or the second pipe 43 to the first adsorption towers 12 and 13 as adsorbent regeneration gas.

2 8は高圧精留塔 2 3の上方に設けられた低圧精留塔 （棚段式またはパックド カラム式） であり、 高圧精留塔 2 3の底部に溜まる液体の高濃度酸素含有液体空 気 2 4が膨脹弁 2 9 a付き送給パイ.プ 2 9を経て送り込まれ ¾。 この低圧精留塔 2 8には、 その底部に凝縮器 3 0力設けられており、 そこに、 高圧精留塔 2 3か ら取り出された窒素ガスの一部が第 1還流用パイプ 3 1を介して導入される。 こ の窒素ガスは、 低圧精留塔 2 8の底部に溜まる液体酸素 （L 0 2 ：純度 9 9 . 7 体積％程度） 3 4を加温して液体酸素 3 4を気ィヒさせる働きをし、 それ自身は液 体酸素 3 4の冷熱によって液化し、 その一部が、 先に述べたように、 流量調整弁 3 2 a付き第 2還流用パイプ 3 2を通って高圧精留塔 2 3の上部に還流し還流液 となる。 また、上記液体窒素 3 4の残部は、 流量調整弁 3 3 a付き分岐パイプ 3 3を通って低圧精留塔 2 8の上部に導入され還流液となって低圧精留塔 2 8内を 流下し気液分離作用をする。 3 5は低圧精留塔 2 8の下部側から延びる製品酸素 ガス取出パイプであり、 低圧精留塔 2 8の底部に溜まる液体酸素 3 4力、ら気ィ匕し た高純度の酸素ガスを取り出して主熱交換器 2 1内に案内し、 高濃度酸素含有圧 縮空気 Yと熱交換させて常温にし製品酸素ガスとして装置外に送り出す作用をす る。 3 6は低圧精留塔 2 8の上部から延びる製品窒素ガス取出パイプであり、低 圧精留塔 2 8の上部に上昇してきた窒素ガスを取り出して主熱交換器 2 1に送り 、 高濃度酸素含有圧縮空気 Yを冷却させるとともに、 それ自身を常温に昇温させ 製品窒素ガスとして装置外に送り出す作用をする。 図において、 3 9はコールド ボックスであり、 内部に、 低温断熱に用いられるパーライト等の断熱材 （図示せ ず） が詰められている。 なお、 この実施の形態では、第 1吸着塔 2， 3のライン は、 窒素ガス吸着により酸素を濃縮しているが、酸素ガスを吸着する吸着剤を用 い、 P及着剤に吸着され濃縮された酸素ガスを取り出すようにしてもよい。 Reference numeral 28 denotes a low-pressure rectification tower (shelf-type or packed-column type) provided above the high-pressure rectification tower 23. 24 is sent through a feed pipe 29 with an expansion valve 29a. The low-pressure rectification column 28 is provided with a condenser 30 at the bottom, and a part of the nitrogen gas extracted from the high-pressure rectification column 23 is supplied to the first reflux pipe 31 1 Introduced via Nitrogen gas This, liquid oxygen accumulated in the bottom of the lower pressure rectification column 2 8 (L 0 2:. Purity 9 9 about 7 vol%) 3 4 serve to warming liquid oxygen 3 4 into gas inhibit the And the liquid itself As described above, a part of the oxygen is liquefied by the cold heat of the body oxygen 34, and a part of the liquid is returned to the upper part of the high-pressure rectification column 23 through the second reflux pipe 32 with the flow control valve 32a. It becomes a reflux liquid. The remaining liquid nitrogen 34 is introduced into the upper part of the low-pressure rectification tower 28 through a branch pipe 33 with a flow control valve 33 a and becomes a reflux liquid and flows down the low-pressure rectification tower 28. It acts as a gas-liquid separator. Reference numeral 35 denotes a product oxygen gas extraction pipe extending from the lower side of the low-pressure rectification column 28, which is capable of collecting liquid oxygen 34 collected at the bottom of the low-pressure rectification column 28, a high-purity oxygen gas that has been depleted. It is taken out and guided into the main heat exchanger 21 where it exchanges heat with the high-concentration oxygen-containing compressed air Y to bring it to room temperature and send it out as oxygen product gas outside the equipment. Reference numeral 36 denotes a product nitrogen gas extraction pipe extending from the upper part of the low-pressure rectification tower 28, which takes out the nitrogen gas that has risen to the upper part of the low-pressure rectification tower 28 and sends it to the main heat exchanger 21 to have a high concentration. Cools the oxygen-containing compressed air Y, raises itself to room temperature, and sends it out as nitrogen gas to the outside of the device. In the figure, reference numeral 39 denotes a cold box, in which heat insulating material (not shown) such as perlite used for low-temperature heat insulation is packed. In this embodiment, the lines of the first adsorption towers 2 and 3 concentrate oxygen by adsorbing nitrogen gas, but use an adsorbent that adsorbs oxygen gas. The removed oxygen gas may be taken out.

この装置を用い、 つぎのようにして窒素ガスおよび酸素ガスを製造することが できる。 すなわち、 まず、 空気圧縮機 （空気圧縮手段） 1から外部の空気を取り 入れ、 ここで空気を低圧で圧縮し、水分離器 （図示せず） により圧縮された空気 中の水分を除去し、 その状態で第 1吸着塔 （酸素濃縮手段） 2 , 3に送り込み、 圧縮空気中の窒素ガス， 7分， 炭酸ガスおよび炭化水素ガス （C n Hm ) 等を吸 着除去する。 これにより、 圧縮空気中の酸素ガスを濃縮する。 これが、 本発明の 最大の特徵である。 ついで、 第 1吸着塔 2， 3を経た高濃度酸素含有圧縮空気 X を酸素空気圧縮機 （酸素空気圧縮手段） 1 1に導入し、 この酸素空気圧縮機 1 1 により高濃度酸素含有圧縮空気 Xをさらに圧縮し高濃度酸素含有圧縮空気 Yとし たのち第 2 P及着塔 1 2 , 1 3に送り込み、高濃度酸素含有圧縮空気 Y中の水， 炭 酸ガスおよび N O x等を吸着除去する。 つぎに、 水， 炭酸ガスおよび Ν Ο χ等が 吸着除去された高濃度酸素含有圧縮空気 Υを主熱交換器 2 1内に送り込んで超低 温に冷却し、 その状態で高圧精留塔 2 3の下部に導入する。 ついで、高圧精留塔 2 3内で、 この高濃度酸素含有圧縮空気 Yと、 氐圧精留塔 2 8でつくられた還流 液体とを向流接触させて圧縮空気を精留し、窒素と酸素の沸点の差 （酸素の大気 ■圧での沸点一 1 83°C， 同じく窒素の沸点一 1 9 6°C) により、 高濃度酸素含有 圧縮空気 Y中の高沸点成分である酸素を液化させ、 窒素を気体とする。 この窒素 ガスを窒素ガス取出パイプ 2 6から取り出して主熱交換器 2 1に送り込んだのち 、 膨脹タービン 3 7に供給し、 ここで寒冷を発生させたのち、 その大部分を装置 外に放出し、一部を第 2吸着塔 1 2， 1 3の再生ガスとする。 Using this apparatus, nitrogen gas and oxygen gas can be produced as follows. That is, first, outside air is taken in from the air compressor (air compression means) 1, where the air is compressed at a low pressure, and the water in the compressed air is removed by a water separator (not shown). in this state fed first adsorption tower (oxygen concentration means) 2, 3, nitrogen gas in the compressed air, 7 minutes, to adsorption removal of carbon dioxide and hydrocarbon gas (C n H m) and the like. Thereby, oxygen gas in the compressed air is concentrated. This is the greatest feature of the present invention. Then, the high-concentration oxygen-containing compressed air X that has passed through the first adsorption towers 2 and 3 is introduced into an oxygen-air compressor (oxygen-air compression means) 11, and the high-concentration oxygen-containing compressed air X is further compressed After the high-concentration oxygen-containing compressed air Y fed to the 2 P及着tower 1 2, 1 3, for adsorbing and removing hyperoxia water containing compressed air Y, carbonated gas and NO x etc. . Next, the high-concentration oxygen-containing compressed air さ れ from which water, carbon dioxide, and Ν χ Ο have been adsorbed and removed is sent into the main heat exchanger 21 and cooled to an extremely low temperature. Introduce at the bottom of 3. Next, the high pressure rectification column In 23, this high-concentration oxygen-containing compressed air Y is brought into countercurrent contact with the reflux liquid produced in the low-pressure rectification column 28 to rectify the compressed air, and the difference between the boiling points of nitrogen and oxygen ( Atmosphere of oxygen I do. This nitrogen gas is taken out from the nitrogen gas extraction pipe 26, sent to the main heat exchanger 21 and then supplied to the expansion turbine 37, where cold is generated, and most of it is discharged outside the device. Part of the gas is used as the regeneration gas for the second adsorption towers 12 and 13.

また、低圧精留塔 2 8の上部に溜まった窒素ガスを製品窒素ガス取出パイプ 3 6から取り出して主熱交換器 2 1に送り込み、 常温近くまで昇温させたのち、 製 品窒素ガスとして装置外に送り出す。 他方、 高圧精留塔 2 3の底部に溜った液体 の高濃度酸素含有液体空気 2 4を送給パイプ 2 9を経て低圧精留塔 2 8に送り込 み、 窆素を気化除去した液体酸素 3 4として低圧精留塔 2 8の底部に溜め、 低圧 精留塔 2 8底部の凝縮器 3 0を通る窒素ガスと熱交換させて気化させる。 この気 化させた酸素ガスを製品酸素ガス取出パイプ 3 5から取り出して主熱交換器 2 1 に送り込み常温近くまで昇温させたのち、 製品酸素ガスとして装置外に送り出す このようにして製品酸素ガスおよび窒素ガスが得られる。  Also, the nitrogen gas collected at the upper part of the low-pressure rectification tower 28 is taken out from the product nitrogen gas extraction pipe 36 and sent to the main heat exchanger 21 where it is heated to near normal temperature and then converted to product nitrogen gas. Send out. On the other hand, liquid oxygen containing high-concentration oxygen, which is a liquid stored at the bottom of the high-pressure rectification column 23, is sent to the low-pressure rectification column 28 via the supply pipe 29, and the liquid oxygen from which nitrogen is vaporized and removed. It is stored at the bottom of the low-pressure rectification tower 28 as 3 4 and is vaporized by heat exchange with nitrogen gas passing through the condenser 30 at the bottom of the low-pressure rectification tower 28. The vaporized oxygen gas is taken out of the product oxygen gas extraction pipe 35, sent to the main heat exchanger 21 and heated to near normal temperature, and then sent out of the apparatus as product oxygen gas. And nitrogen gas.

上記実施の形態では、 第 1吸着塔 2， 3により、 圧縮空気中の酸素ガスの濃度 が 2 0. 9体積％力、ら 5 0体積％程度に濃縮されているため、 1 0， 0 0 0 m3 /h (No rma l) の酸素ガスを製造するのに必要な空気量は、酸素ガスの回 収効率を 9 7 %とすると、 理論上では、 空気量 = ( 1 0, 0 0 0 ÷ 0. 5 0 0 ) ÷ 0. 9 7で算出され、 約 2 0， 6 0 Om3 /h (No rma 1 ) の空気量であ り、 冒頭で述べた従来のものの 4 1%程度に減少している。 しかも、 1 0, 0 0 Om3 /h (No rma 1) の酸素ガスを製造するのに必要な酸素空気圧縮機 1 1の圧縮動力が 2 0 0 0 kW程度にまで減少し、 また、 酸素空気圧縮機 1の圧縮 動力が 3 0 0 kW程度に、 真空ポンプ 4の駆動動力が 9 0 0 kW程度に、 電気ヒ —夕 4 1の電力量が 2 0 0 kW程度になると推測されるため、 合計 3 4 0 0 kW となり、従来の 7 0%程度に減少している。 したがって、 3 0%以上の省エネル ギ一を実現できる。 In the above embodiment, the concentration of oxygen gas in the compressed air is reduced to about 20.9 vol. The amount of air required to produce 0 m 3 / h (No rmal) oxygen gas is theoretically the air amount = (10, 00), assuming that the oxygen gas recovery efficiency is 97%. 0 ÷ 0.50 0) ÷ Calculated from 0.97, which is about 20, 60 Om 3 / h (No rma 1), which is about 41% of the conventional one described at the beginning. Has decreased. In addition, the compression power of the oxygen-air compressor 11 required to produce 100,000 Om 3 / h (No rma 1) oxygen gas is reduced to about 2000 kW, and the oxygen Because it is estimated that the compression power of the air compressor 1 will be about 300 kW, the driving power of the vacuum pump 4 will be about 900 kW, and the electric power of the electric pump 4 will be about 200 kW. 340 kW, which is about 70% of the conventional level. Therefore, energy saving of 30% or more can be realized.

また、 この実施の形態では、 原料空気を圧縮する空気圧縮機 1に続いて、 その 圧縮空気中の酸素ガスを濃縮する第 1吸着塔 2， 3を設け、 原料空気中の酸素濃 度を高め、 これを酸素空気圧縮機 1 1, 主熱交換器 2 1を経由して高圧精留塔 2 3, 低圧精留塔 2 8に供給している。 そのため、 酸素空気圧縮機 1 1以降の、 主 熱交換器 2 1, 両精留塔 2 3, 2 8のような各機器の流通流量の大幅な低減を実 現することにより、 それらを従来のものの半分以下に小形化でき、 結果的に装置 全体の著し 、小形化を達成することができる。 Further, in this embodiment, following the air compressor 1 for compressing the raw material air, First adsorption towers 2 and 3 for concentrating oxygen gas in the compressed air are provided to increase the oxygen concentration in the raw material air, which is passed through the oxygen-air compressor 11 and the main heat exchanger 21 to high-pressure purification. Distillation tower 23, low-pressure rectification tower 28 Therefore, by realizing a drastic reduction in the flow rate of each device such as the main heat exchanger 21 and the two rectification columns 23 and 28 after the oxygen-air compressor 11, The size of the device can be reduced to less than half, and as a result, the entire device can be significantly reduced in size.

例えば、 7 0， 0 0 Om3 /h (No rma 1 ) の酸素ガスを製造する場合、 従来のものでは高圧精留塔 2 3の直径が 7 m (当社計算値） となり、 これは工場 で組立てて現地に運ぶのは輸送手段がないこと力ヽら、 やむなく現地で組立てざる を得なかったが、 この実施の形態では、 同量の酸素を製造する場合、精留塔を流 通する気体が 1 / 2以下となるため、上記精留塔の直径を約 4. 2 mにすること ができる。 そのため、 工場で組立て現地に運搬することが可能となり、大幅な省 力化が可能となる。 For example, when producing 70,000 Om 3 / h (No rma 1) oxygen gas, the diameter of the high-pressure rectification column 23 is 7 m (calculated by our company) with the conventional one, which is It was necessary to assemble on-site because there was no transportation means to assemble and transport it to the site, but in this embodiment, when producing the same amount of oxygen, the gas flowing through the rectification column Is less than 1/2, the diameter of the rectification column can be reduced to about 4.2 m. As a result, it is possible to assemble the products at the factory and transport them to the site, which can save a great deal of labor.

図 2は本発明の空気分離装置の他の実施の形態を示している。 この実施の形態 では、 第 2吸着塔 1 2， 1 3を省いている。 すなわち、 第 2吸着塔 1 2， 1 3, 第 2放出パイプ 1 4， 開閉弁 1 6 a， 1 6 b, 1 7 a, 1 7 b, 1 8 a, 1 8 b ； 1 9 a， 1 9 b付きのパイプ路， 分岐パイプ 4 0および第 1〜第 3パイプ 42 ~4 4を省いている。 それ以外の部分は上記実施の形態と同様であり、 同様の部 分には同じ符号を付している。 この実施の形態では、 装置を、 原料空気として清 浄な空気を用いるような場所等に設置することにより、 前記実施の形態と同様の 効果を奏するうえ、装置の簡素化， 小形化を達成できる。  FIG. 2 shows another embodiment of the air separation device of the present invention. In this embodiment, the second adsorption towers 12 and 13 are omitted. That is, the second adsorption towers 12 and 13, the second discharge pipe 14, the on-off valves 16a, 16b, 17a, 17b, 18a, 18b; 19a, 1 The pipe line with 9b, the branch pipe 40 and the first to third pipes 42 to 44 are omitted. Other parts are the same as those in the above embodiment, and the same parts are denoted by the same reference numerals. In this embodiment, by installing the device in a place where clean air is used as raw material air, the same effects as in the above embodiment can be obtained, and the device can be simplified and downsized. .

図 3は本発明の空気分離装置のさらに他の実施の形態を示している。 この実施 の形態では、 図 2に示す実施の形態において、 膨脹タービン 3 7に代えて、 装置 外からタンク口一リー等で液体酸素 （L02 ) が供給される液体酸素貯槽 （図示 せず) を用い、 その液体酸素を寒冷源としている以外は、 実質的に図 2に示す装 置と同じである。 図において、 4 7は液体酸素貯槽からの液体酸素を、 寒冷源と して低圧精留塔 2 8の下部に導入する導入パイプであり、 この導入パイプ 4 7か ら導入された液体酸素が低圧精留塔 2 8の底部に流下し、 この底部に溜まる液体 酸素 3 4に合流する。 48は低圧精留塔 2 8から延びる排出用パイプであり、 低 圧精留塔 2 8の棚段 （またはパックドカラム） 2 8 aの上部に溜まる窒素ガス （ 廃 G N 2 ) を取り出して過冷却器 4 9に導入し、 この過冷却器 4 9を経た廃窒素 ガスを主熱交換器 2 1内に案内し、 高濃度酸素含有圧縮空気 Yを冷却したのち外 部に放出する作用をする。 上記過冷却器 4 9は、 その内部に、 送給パイプ 2 9内 の高濃度酸素含有液体空気 2 4、 分岐パイプ 3 3内の液体窒素 （還流液） 、 製品 窒素ガス取出パイプ 3 6内の製品窒素ガスおよび排出用パイプ 4 8内の廃窒素ガ スを通し、 送給パイプ 2 9内の高濃度酸素含有液体空気 2 4を冷却する作用をす る。 5 0は低圧精留塔 2 8の底面から延びる液体酸素取出パイプであり、 低圧精 留塔 2 8の底部に溜まる液体酸素を取り出して主熱交換器 2 1内に案内し、 高濃 度酸素含有圧縮空気 Yを冷却させるとともに、 それ自身を常温に昇温させ製品酸 素ガスとして製品酸素ガス取出パイプ 3 5に導入する作用をする。 5 1は製品窒 素ガス取出パイプ 3 6に設けた製品窒素ガス圧縮機であり、 製品窒素ガス取出パ イブ 3 6内を通る製品窒素ガスを所定の圧力に昇圧する作用をする。 5 2は製品 酸素ガス取出パイプ 3 5に設けた第 1製品酸素ガス圧縮機であり、 製品酸素ガス 取出パイプ 3 5内を通る製品酸素ガスを所定の圧力に昇圧し低圧製品酸素ガス取 出パイプ 5 3に供給する作用をする。 5 4は第 2製品酸素ガス圧縮機であり、 第 1;製品酸素ガス圧縮機 5 2を経た製品酸素ガスをさらに昇圧し高圧製品酸素ガス 取出パイプ 5 5に供給する作用をする。 なお、 この実施の形態では、 高圧精留塔FIG. 3 shows still another embodiment of the air separation device of the present invention. In this embodiment, in the embodiment shown in FIG. 2, instead of the expansion turbine 37, a liquid oxygen storage tank (not shown) in which liquid oxygen (L0 2 ) is supplied from outside the apparatus by a tank opening or the like. The apparatus is substantially the same as the apparatus shown in FIG. 2, except that the liquid oxygen is used as a cold source. In the figure, reference numeral 47 denotes an introduction pipe for introducing the liquid oxygen from the liquid oxygen storage tank to the lower part of the low-pressure rectification column 28 as a cold source. It flows down to the bottom of the rectification column 28 and joins the liquid oxygen 34 collected at this bottom. 48 is a discharge pipe extending from the low-pressure rectification column 28, The nitrogen gas (waste GN 2 ) collected at the upper part of the tray (or packed column) 28 a of the pressure rectification tower 28 is taken out, introduced into the supercooler 49, and the waste nitrogen passed through the supercooler 49. The gas is guided into the main heat exchanger 21 and acts to discharge the compressed air Y containing high concentration oxygen after cooling. The supercooler 49 is provided with high-concentration oxygen-containing liquid air 24 in the supply pipe 29, liquid nitrogen (reflux liquid) in the branch pipe 33, and products in the nitrogen gas extraction pipe 36. The high-concentration oxygen-containing liquid air 24 in the supply pipe 29 is cooled by passing the product nitrogen gas and the waste nitrogen gas in the discharge pipe 48. Reference numeral 50 denotes a liquid oxygen extraction pipe extending from the bottom of the low-pressure rectification tower 28, which takes out the liquid oxygen collected at the bottom of the low-pressure rectification tower 28 and guides it into the main heat exchanger 21 to produce high-concentration oxygen. While cooling the contained compressed air Y, it acts to raise itself to room temperature and introduce it into the product oxygen gas extraction pipe 35 as product oxygen gas. Reference numeral 51 denotes a product nitrogen gas compressor provided in the product nitrogen gas extraction pipe 36, which acts to increase the product nitrogen gas passing through the product nitrogen gas extraction pipe 36 to a predetermined pressure. Reference numeral 2 denotes a first product oxygen gas compressor provided in the product oxygen gas extraction pipe 35, and the product oxygen gas passing through the product oxygen gas extraction pipe 35 is pressurized to a predetermined pressure to obtain a low-pressure product oxygen gas extraction pipe. It acts to supply 5 3. 5 4 is a second oxygen product gas compressor, first, to the effect supplied to the high pressure product oxygen gas takeout pipe 5 5 further boost the product oxygen gas through the oxygen product gas compressor 5 2. In this embodiment, the high-pressure rectification column

2 3の天井面と、 この高圧精留塔 2 3の上方に設けた低圧精留塔 2 8の底面とを 一体化し同一材で形成している。 図において、 3 6 aは製品窒素ガス取出パイプThe ceiling surface of 23 and the bottom surface of the low-pressure rectification tower 28 provided above the high-pressure rectification tower 23 are integrated and formed of the same material. In the figure, 36a is the product nitrogen gas extraction pipe

3 6内を通る製品窒素ガスを排出用パイプ 4 8に送給するパイプである。 3 9 A はコールドボックスであり、 内部にパーライト等の断熱材が充塡され真空吸弓 [さ れている。 それ以外の部分は、 図 2に示す実施の形態と同様であり、 同様の部分 には同じ符号を付している。 A pipe for supplying product nitrogen gas passing through 36 to a discharge pipe 48. 39 A is a cold box, which is filled with a heat insulating material such as pearlite and has a vacuum suction. Other parts are the same as those of the embodiment shown in FIG. 2, and the same parts are denoted by the same reference numerals.

この装置を用い、 つぎのようにして窒素ガスおよび酸素ガスを製造することが できる。 すなわち、 図 2に示す実施の形態と同様にし、 空気圧縮機 （空気圧縮手 段） 1から外部の空気を取り入れ、 ここで空気を低圧で圧縮し、 zK分離器 （図示 せず） により圧縮された空気中の水分を除去し、 その状態で第 1吸着塔 （酸素濃 縮手段） 2， 3に送り込み、 圧縮空気中の窒素ガス， 水分， 炭酸ガスおよび炭化 水素ガス （C n Hm ) 等を吸着除去する。 これにより、圧縮空気中の酸素ガスを 濃縮する。 ついで、第 1 P及着塔 2， 3を経た高濃度酸素含有圧縮空気 Xを酸素空 気圧縮機 （酸素空気圧縮手段） 1 1に導入し、 この酸素空気圧縮機 1 1により高 濃度酸素含有圧縮空気 Xをさらに圧縮し高濃度酸素含有圧縮空気 Yとする。 つぎ に、 この高濃度酸素含有圧縮空気 Yを主熱交換器 2 1内に送り込んで超低温に冷 却し、 その状態で高圧精留塔 2 3の下部に導入する。 ついで、 高圧精留塔 2 3内 で、 この高濃度酸素含有圧縮空気 Yと、 低圧精留塔 2 8でつくられた還流液体と を向流接触させて圧縮空気を精留し、 窒素と酸素の沸点の差 （酸素の大気圧での 沸点一 1 8 3 °C, 同じく窒素の沸点— 1 9 6 °C) により、 高濃度酸素含有圧縮空 気 Y中の高沸点成分である酸素を液化させ、 窒素を気体とする。 Using this apparatus, nitrogen gas and oxygen gas can be produced as follows. That is, in the same manner as in the embodiment shown in FIG. 2, external air is taken in from an air compressor (air compression means) 1, where the air is compressed at a low pressure and compressed by a zK separator (not shown). The moisture in the compressed air is removed and sent to the first adsorption tower (oxygen concentrating means) 2 and 3 in that state, and the nitrogen gas, moisture, carbon dioxide gas and carbonized gas in the compressed air are removed. Hydrogen gas (C n H m) and the like are adsorbed and removed. This enriches the oxygen gas in the compressed air. Next, the high-concentration oxygen-containing compressed air X that has passed through the first P and the landing towers 2 and 3 is introduced into an oxygen-air compressor (oxygen-air compression means) 11, and the oxygen-air compressor 11 generates high-concentration oxygen-containing air. Compressed air X is further compressed to obtain high-concentration oxygen-containing compressed air Y. Next, the high-concentration oxygen-containing compressed air Y is sent into the main heat exchanger 21 to be cooled to an extremely low temperature, and then introduced into the lower part of the high-pressure rectification column 23 in that state. Then, in the high-pressure rectification column 23, the high-concentration oxygen-containing compressed air Y and the reflux liquid produced in the low-pressure rectification column 28 are brought into countercurrent contact to rectify the compressed air, thereby obtaining nitrogen and oxygen. Liquefaction of oxygen, which is a high-boiling component in high-concentration oxygen-containing compressed air Y, due to the difference in boiling point of oxygen (boiling point of oxygen at atmospheric pressure-18 ° C, also boiling point of nitrogen-196 ° C) To make nitrogen gas.

また、 低圧精留塔 2 8の上部に溜まった窒素ガスを製品窒素ガス取出パイプ 3 6から取り出して過冷却器 （熱交換器） 4 9に送り込み、主熱交換器 2 1に導入 して主熱交換器 2 1で常温近くまで昇温させたのち、 製品窒素ガスとして装置外 に送り出す。 他方、 高圧精留塔 2 3の底部に溜った高濃度酸素含有液体空気 2 4 を送給パイプ 2 9で過冷却器 4 9に送り込み、 ここで冷却した気一液混合状態の 高濃度酸素含有液体空気 2 4を低圧精留塔 2 8に送り込み、 窒素を気化除去した 液体酸素 3 4として低圧精留塔 2 8の底部に溜め、 低圧精留塔 2 8底部の凝縮器 3 0を通る窒素ガスと熱交換させて気化させる。 この気化させた酸素ガスを製品 酸素ガス取出パイプ 3 5から取り出して主熱交換器 2 1に送り込み常温近くまで 昇温させたのち、 第 1製品酸素圧縮機 5 2を経由した製品酸素ガスを低圧製品酸 素ガス取出パイプ 5 3により装置外に送り出し、 第 2製品酸素圧縮機 5 4を経由 した製品酸素ガスを高圧製品酸素ガス取出パイプ 5 5により装置外に送り出す。 このようにして製品酸素ガスおよび窒素ガスが得られる。  The nitrogen gas collected at the top of the low-pressure rectification column 28 is taken out from the product nitrogen gas extraction pipe 36, sent to the supercooler (heat exchanger) 49, and introduced into the main heat exchanger 21. After the temperature is raised to near normal temperature in the heat exchanger 21, it is sent out of the equipment as product nitrogen gas. On the other hand, the high-concentration oxygen-containing liquid air 24 collected at the bottom of the high-pressure rectification column 23 is sent to the supercooler 49 via the supply pipe 29, where the high-concentration oxygen containing the cooled gas-liquid mixture is contained. The liquid air 24 is sent to the low-pressure rectification tower 28, and the nitrogen is vaporized and removed.The liquid oxygen 34 is stored at the bottom of the low-pressure rectification tower 28, and the nitrogen passes through the condenser 30 at the bottom of the low-pressure rectification tower 28. It is vaporized by heat exchange with gas. The vaporized oxygen gas is taken out from the product oxygen gas extraction pipe 35, sent to the main heat exchanger 21 and heated to near normal temperature, and then the product oxygen gas passed through the first product oxygen compressor 52 is reduced in pressure. The product oxygen gas is sent out of the device by the product oxygen gas extraction pipe 53, and the product oxygen gas that has passed through the second product oxygen compressor 54 is sent out of the device by the high-pressure product oxygen gas extraction pipe 55. In this way, product oxygen gas and nitrogen gas are obtained.

上記のように、 この実施の形態でも、 図 2の実施の形態と同様の作用 ·効果を 3#."5る。  As described above, also in this embodiment, the same operation and effect as in the embodiment of FIG.

図 4は本発明の空気分離装置のさらに他の実施の形態を示している。 この実施 の形態では、 図 2に示す実施の形態において、 膨脹夕一ビン 3 7に代えて、 装置 外からタンクローリ一等で液体窒素 （L N 2 ) が供給される液体窒素貯槽 （図示 せず） を用い、 その液体窒素を寒冷源としている以外は、 実質的に図 2に示す装 置と同じである。 すなわち、 4 7 aは液体窒素貯槽からの液体窒素を、 寒冷源と して高圧精留塔 2 3の上部に導入する導入パイプであり、 この導入パイプ 4 7 a カヽら導入された液体窒素と低圧精留塔 2 8下部の凝縮器 3 0で液化された液体窒 素の一部とが、 高圧精留塔 2 3の上部に導入される。 それ以外の部分は、 図 2に 示す実施の形態と同様であり、 同様の部分には同じ符号を付している。 FIG. 4 shows still another embodiment of the air separation device of the present invention. In this embodiment, in the embodiment shown in FIG. 2, a liquid nitrogen storage tank (not shown) in which liquid nitrogen (LN 2 ) is supplied from outside the apparatus by a tank trolley or the like instead of the expansion bottle 37 Except that the liquid nitrogen is used as the cold source. Is the same as That is, 47a is an introduction pipe for introducing the liquid nitrogen from the liquid nitrogen storage tank into the upper part of the high-pressure rectification column 23 as a cold source. Part of the liquid nitrogen liquefied in the condenser 30 at the lower part of the low-pressure rectification tower 28 is introduced into the upper part of the high-pressure rectification tower 23. Other parts are the same as those of the embodiment shown in FIG. 2, and the same parts are denoted by the same reference numerals.

図 5は本発明の空気分離装置のさらに他の実施の形態を示している。 この実施 の形態では、 図 1に示す実施の形態において、 空気圧縮機 1を経た圧縮空気を第 1吸着塔 2， 3に送給する第 1送給パイプ 1 aと、第 1吸着塔 2 , 3を経た高濃 度酸素含有圧縮空気 Xを酸素空気圧縮機 1 1に導入する導入パイプ 5 7 (図 1に は、 符号 5 7を付していない） とを、 開閉弁 （もしくは流量調整弁） 5 8 a付き 連通パイプ 5 8で連通している。 そして、上記開閉弁 5 8 aを開弁し、 空気圧縮 機 1 , 水分離器 （図示せず） を経た圧縮空気の一部を上記連通パイプ 5 8を介し て直接に （すなわち、 第 1吸着塔 2， 3を経由させずに） 導入パイプ 5 7に送り 込むとともに、 残部を第 1吸着塔 2， 3を経由させて導入パイプ 5 7に送り込み 、 この導入パイプ 5 7で両者を合流させて、 連通パイプ 5 8を介して導入パイプ 5 7に導入した圧縮空気の一部で、第 1吸着塔 2 , 3を経由させて導入パイプ 5 7に導入した圧縮空気の残部の酸素ガスの濃度を薄めるようにしている。 それ以 外の部分は、 図 1に示す実施の形態と同様であり、 同様の部分には同じ符号を付 している。 この実施の形態でも、 図 1に示す実施の形態と同様の作用。 効果を 奏する。 しかも、 高圧精留塔 2 3の下部に供給される圧縮空気中の酸素ガスの濃 度が低くなり、 製品酸素ガス量を少なくすることができる。 したがって、 製品酸 素ガス量を低減させたいときには、 これに対応することができる。 なお、 このよ うな開閉弁 5 8 a付き連通パイプ 5 8は、 図 2〜図 4に示す実施の形態において も、 用いることができる。  FIG. 5 shows still another embodiment of the air separation device of the present invention. In this embodiment, in the embodiment shown in FIG. 1, a first feed pipe 1a for feeding compressed air passed through an air compressor 1 to first adsorption towers 2 and 3; The introduction pipe 57 for introducing the highly concentrated oxygen-containing compressed air X passed through 3 into the oxygen-air compressor 11 (not denoted by 57 in FIG. 1) is connected to an on-off valve (or a flow control valve). ) With 58a Communication pipe 58 communicates. Then, the on-off valve 58a is opened, and a part of the compressed air that has passed through the air compressor 1 and the water separator (not shown) is directly passed through the communication pipe 58 (that is, the first adsorbent). (Without passing through the towers 2 and 3) and into the introduction pipe 57 through the first adsorption towers 2 and 3 while the remainder is sent to the introduction pipe 57. A part of the compressed air introduced into the introduction pipe 57 through the communication pipe 58, the concentration of oxygen gas in the remaining compressed air introduced into the introduction pipe 57 through the first adsorption towers 2 and 3 is reduced. I try to dilute it. Other parts are the same as those of the embodiment shown in FIG. 1, and the same parts are denoted by the same reference numerals. In this embodiment, the operation is the same as that of the embodiment shown in FIG. It works. Moreover, the concentration of the oxygen gas in the compressed air supplied to the lower part of the high-pressure rectification column 23 is reduced, and the amount of the product oxygen gas can be reduced. Therefore, when it is desired to reduce the amount of product oxygen gas, this can be dealt with. Note that such a communication pipe 58 with the on-off valve 58a can be used also in the embodiment shown in FIGS.

Claims

請求の範囲 The scope of the claims 1 . 外部より空気を取り入れて低圧で圧縮する空気圧縮手段と、 この空気圧縮手 段によって圧縮された圧縮空気中の酸素ガスを濃縮する酸素濃縮手段と、 この酸 素濃縮手段を経た高濃度酸素含有圧縮空気 Xをさらに圧縮する酸素空気圧縮手段 と、 この酸素空気圧縮手段を経た高濃度酸素含有圧縮空気 Yを冷却する熱交換器 と、 この熱交換器を経由し低温に冷却された高濃度酸素含有圧縮空気 Yを各成分 ガスの沸点差を利用して分離し酸素ガスを取り出す精留塔とを備えたことを特徴 とする空気分離装置。 1. Air compression means for taking in air from outside and compressing it at low pressure, oxygen concentrating means for concentrating oxygen gas in compressed air compressed by this air compression means, and high-concentration oxygen passing through this oxygen concentrating means Oxygen-air compression means for further compressing the compressed air containing X, heat exchanger for cooling the high-concentration oxygen-containing compressed air Y having passed through the oxygen-air compression means, and high-concentration cooled to low temperature via this heat exchanger An air separation device comprising: a rectification column that separates oxygen-containing compressed air Y by utilizing a difference in boiling points of respective component gases to extract oxygen gas. 2 . 上記酸素濃縮手段を、 圧縮空気中の窒素ガスを吸着する吸着剤を収容する吸 着塔とし、 上記吸着剤で圧縮空気中の水分等の不純物をも除去するようにした請 求項 1記載の空気分離装置。  2. Claim 1 in which the oxygen concentrating means is an adsorption tower containing an adsorbent for adsorbing nitrogen gas in compressed air, and the adsorbent also removes impurities such as moisture in the compressed air. An air separation device as described. 3 . 酸素空気圧縮手段と熱交換器との間に、 高濃度酸素含有圧縮空気 Y中の不純 物を除去する除去手段を設けた請求項 1または 2記載の空気分離装置。  3. The air separation device according to claim 1, further comprising a removal means for removing impurities in the high-concentration oxygen-containing compressed air Y between the oxygen-air compression means and the heat exchanger. 4 . 酸素濃縮手段を経た高濃度酸素含有圧縮空気 Xを酸素空気圧縮手段に導入す る導入路に、 空気圧縮手段によつて圧縮された圧縮空気の一部を、 酸素濃縮手段 を経由させることなく、 直接供給するようにした請求項 1〜 3のいずれか一項に 記載の空気分離装置。  4. A part of the compressed air compressed by the air compressor is passed through the oxygen concentrator in the introduction path for introducing the high-concentration oxygen-containing compressed air X passed through the oxygen concentrator into the oxygen air compressor. The air separation device according to any one of claims 1 to 3, wherein the air separation device is supplied directly.
PCT/JP2004/004145 2003-03-26 2004-03-25 Air separator Ceased WO2004085941A1 (en)

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