JP4782380B2 - Air separation device - Google Patents
Air separation device Download PDFInfo
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- JP4782380B2 JP4782380B2 JP2004002877A JP2004002877A JP4782380B2 JP 4782380 B2 JP4782380 B2 JP 4782380B2 JP 2004002877 A JP2004002877 A JP 2004002877A JP 2004002877 A JP2004002877 A JP 2004002877A JP 4782380 B2 JP4782380 B2 JP 4782380B2
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- Prior art keywords
- air
- oxygen
- gas
- compressed air
- heat exchanger
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- 238000000926 separation method Methods 0.000 title claims description 31
- 239000001301 oxygen Substances 0.000 claims description 93
- 229910052760 oxygen Inorganic materials 0.000 claims description 93
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 92
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 92
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 72
- 229910001882 dioxygen Inorganic materials 0.000 claims description 57
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 52
- 238000001179 sorption measurement Methods 0.000 claims description 51
- 230000006835 compression Effects 0.000 claims description 32
- 238000007906 compression Methods 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 30
- 229910052757 nitrogen Inorganic materials 0.000 claims description 20
- 239000003463 adsorbent Substances 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 10
- 239000002912 waste gas Substances 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims 1
- 150000002926 oxygen Chemical class 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 238000000605 extraction Methods 0.000 description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 description 8
- 239000001569 carbon dioxide Substances 0.000 description 8
- 238000010992 reflux Methods 0.000 description 8
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 229910052786 argon Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000011810 insulating material Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- -1 moisture Chemical compound 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910001562 pearlite Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 206010058490 Hyperoxia Diseases 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 230000000222 hyperoxic effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/50—Oxygen
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
- Drying Of Gases (AREA)
Description
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。 The present invention relates to an air separation device capable of producing oxygen gas with energy saving and significantly miniaturizing the device.
一般に、窒素ガス（ＧＮ2），酸素ガス（ＧＯ2），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６１で圧縮したのち、吸着塔６２に入れて圧縮空気中の水（Ｈ2Ｏ），炭酸ガス（ＣＯ2）および炭化水素ガス（ＣnＭm）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６２の再生用として利用されている（例えば、特許文献１参照）。図６において、６４は再生・排気用のヒーターである。
このような空気分離装置では、空気圧縮機６１として、通常、吐出圧力が５ｋｇ／ｃｍ2Ｇ〔０．５ＭＰａＧ（ゲージ圧）〕程度の空気圧縮機６１が使用されているが、この空気圧縮機６１を用いて１０，０００ｍ3／ｈ（Ｎｏｒｍａｌ）の酸素ガスを製造しようとすると、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％）が、酸素２０．９％：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＝（１０，０００÷０．２０９）÷０．９７で算出され、約５０，０００ｍ3／ｈ（Ｎｏｒｍａｌ）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っている。しかも、１０，０００ｍ3 ／ｈ（Ｎｏｒｍａｌ）の酸素ガスを製造する場合、これに必要な空気圧縮機６１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０．０９を乗じた値とされている）が４５００ｋＷ程度であり、吸着塔６２の再生・排気用のヒーター６４の駆動動力が５００ｋＷ程度であるため、合計５０００ｋＷ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 [0.5 MPaG (gauge pressure)] is usually used as the air compressor 61. When oxygen gas of 10,000 m 3 / h (Normal) is produced using 61, the amount of air necessary for this is as follows: component ratio (volume%) of each component gas of air is oxygen 20.9%: Nitrogen 78.1%: Argon 0.9%. Therefore, assuming that the recovery efficiency of oxygen gas is 97%, the amount of air is theoretically calculated by (10,000 ÷ 0.209) ÷ 0.97. An air amount of about 50,000 m 3 / h (Normal) is required. For this reason, it is necessary to use an adsorption tower 62, a main heat exchanger, a rectifying tower, etc. that match the required amount of air, and the entire apparatus becomes large. In addition, when producing oxygen gas of 10,000 m 3 / h (Normal), the compression power of the air compressor 61 required for this (this compression power is usually about 0.09 in the numerical value of the required air amount). Is about 4500 kW, and the driving power of the regeneration / exhaust heater 64 of the adsorption tower 62 is about 500 kW, which requires a large amount of power of about 5000 kW in total and produces oxygen gas. It takes a lot of energy.
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。 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 can greatly reduce the size of a cryogenic separation mechanism (cold box and its internal equipment). Is the purpose.
上記の目的を達成するため、本発明の空気分離装置は、外部より原料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空気分離装置であって、上記外部より取り入れた原料空気を上記熱交換器を経由して上記精留塔へ供給する導入路に、上記酸素濃縮手段として、上記原料空気中の窒素ガスを吸着する吸着剤が収容された吸着塔を設け、その吸着塔の設けられた原料空気導入路において、上記吸着塔を挟んで上流側に上記空気圧縮手段を設けるとともに、下流側に上記酸素空気圧縮手段を設け、その圧力を利用して、上記高濃度酸素含有圧縮空気Ｙを酸素空気圧縮手段から精留塔側に直接供給可能にし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 means for taking in raw material air from the outside and compressing the raw material air at a low pressure, and an oxygen for concentrating oxygen gas in the compressed air compressed by the air compression means. A concentration means, an oxygen air compression means for further compressing the high concentration oxygen-containing compressed air X passed through the oxygen concentration means, a heat exchanger for cooling the high concentration oxygen-containing compressed air Y passed through the oxygen air compression means, and An air separation apparatus comprising: a rectifying tower that separates high-concentration oxygen-containing compressed air Y that has been cooled to a low temperature via a heat exchanger using a difference in boiling point between the component gases and extracts oxygen gas, the feed air taken from the outside to the introduction path for supplying upward KiseiTome column via the heat exchanger, as the oxygen concentration means, the adsorbent for adsorbing nitrogen gas of the feed air is contained adsorbed Set up a tower In feed air introduction path provided thereof adsorption tower, with provision of the air compression means on the upstream side across the adsorption tower, the oxygen air compression means provided on the downstream side, by utilizing the pressure, the high The configuration is such that the compressed air Y containing the concentrated oxygen can be directly supplied from the oxygen air compression means to the rectifying column side .
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、酸素濃縮手段として、上記原料空気中の窒素ガスを吸着する吸着剤が収容された吸着塔を設け、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化でき、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１／１０以下のことをいう。 That is, the air separation unit of the present invention, the feed air is compressed to a low pressure by the air compression means, subsequent to the air compression means, as oxygen concentration means, the adsorbent for adsorbing nitrogen gas of the feed air is An accommodated adsorption tower is provided to increase the oxygen concentration in the raw material air, and this is supplied to the rectification tower via an oxygen air compression means and a heat exchanger. Therefore, when producing the same amount of oxygen gas, etc., it is possible to save a great deal of energy and realize a significant reduction in the flow rate of each means after the oxygen concentrating means, thereby reducing them to less than half of the conventional one. As a result, the overall apparatus can be significantly reduced in size. Here, the low pressure means that the pressure is lower than the compression pressure by the oxygen air compression means. Usually, it is 1/3 or less, preferably 1/5 or less, more preferably, the compression pressure of the oxygen air compression means. 1/10 or less.
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，水分，ＮＯX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、質の悪い空気も利用できるようになる。 Further, when 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. hydrocarbons, water, can be removed NO X, etc., feed air (often sodium ions) along the coast as an air or air (automobile exhaust frequently) along roads, also available poor air quality.
つぎに、本発明の実施の形態を図面にもとづいて詳しく説明する。 Next, embodiments of the present invention will be described in detail with reference to the drawings.
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、０．１ｋｇ／ｃｍ2Ｇ〔０．０１ＭＰａＧ（ゲージ圧）〕程度の低圧に設定されている。１ａは空気圧縮機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、上流側がシリカゲル等の吸着剤が充填され、下流側に当出願人が開発したモレキュラーシーブス製吸着剤（エア・ウォーター社製ＡＷ０２０３）が充填されている。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（Ｈ2Ｏ），炭酸ガス（ＣＯ2）および炭化水素ガス（ＣnＨm）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、４ａ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６ａ，６ｂ，８ａ，８ｂ付きのパイプ路ならびに真空ポンプ４からなる系は、ＶＳＡ（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）は真空ポンプ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ＶＳＡとなっているが、ＰＳＡ（プレッシャースイングアブソープド），ＴＳＡ（サー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、６ａ，６ｂ，７ａ，７ｂ，８ａ，８ｂ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。 FIG. 1 shows an embodiment of the air separation device of the present invention. In the figure, reference numeral 1 denotes an air compressor (air compression means) that takes in and compresses the atmosphere, and its discharge pressure is set to a low pressure of about 0.1 kg / cm 2 G [0.01 MPaG (gauge pressure)]. Yes. Reference numeral 1 a denotes a first feed pipe that feeds compressed air that has passed through the air compressor 1 to the first adsorption towers 2 and 3. The first adsorption towers (oxygen concentrating means) 2 and 3 are filled with an adsorbent such as silica gel on the upstream side, and the molecular sieves adsorbent developed by the present applicant on the downstream side (AW0203 manufactured by Air Water). Is filled. The first adsorption towers 2 and 3 are in pairs and are operated by alternately switching between adsorption and regeneration. In this embodiment, due to 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 For example, oxygen gas is 50%: nitrogen gas is 47.5%: argon gas is about 2.5%, and the concentration of oxygen gas in the compressed air is concentrated from 20.9% to 50% by volume. The first adsorption towers 2 and 3 adsorb and remove water (H 2 O), carbon dioxide gas (CO 2 ), hydrocarbon gas (C n H m ), etc. in the compressed air by the action of the adsorbent simultaneously with the above concentration. To do. 4 is a vacuum pump for regeneration / exhaust of the first adsorption towers 2 and 3, and 4 a is a first discharge pipe that releases and adsorbs the waste gas adsorbed by the adsorbent of the first adsorption towers 2 and 3 to the atmosphere. It acts to regenerate the agent. As described above, the system composed of the first adsorption towers 2 and 3, the pipe passages with the on-off valves 6a, 6b, 8a and 8b and the vacuum pump 4 is VSA (vacuum swing absorbed) and membrane separation. When one first adsorption tower 2 (3) is performing an adsorption operation, the other first adsorption tower 3 (2) is regenerated by vacuum suction of the vacuum pump 4. A water separator (not shown) for removing moisture in the compressed air compressed by the air compressor 1 between the air compressor 1 and the first adsorption towers 2 and 3, depending on circumstances, A Freon cooler (not shown) for cooling the compressed air that has passed through the water separator is provided. In this embodiment, the above system is VSA. However, PSA (pressure swing absorbed) or TSA (thermal swing absorbed) membrane separation may be used. In the figure, 6a, 6b, 7a, 7b, 8a, 8b are on-off valves for alternately adsorbing and regenerating the first adsorption towers 2 and 3.
１１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１／２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１１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ューガルコンプレッサー：吐出圧力５ｋｇ／ｃｍ2Ｇ〔０．５ＭＰａＧ（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。１１ａは酸素空気圧縮機１１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ーブス等の吸着剤が充填され、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っている）であり、酸素空気圧縮機１１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，ＣnＭmおよびＮＯX等を吸着除去する作用をする。１４は第２放出パイプで、第２吸着塔１２，１３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１２，１３および開閉弁１６ａ，１６ｂ，１９ａ，１９ｂ付きのパイプ路からなる系は、ＴＳＡとなっている。図において、１６ａ，１６ｂ，１７ａ，１７ｂ，１８ａ，１８ｂ，１９ａ，１９ｂは第２吸着塔１２，１３を交互に吸着・再生運転させるための開閉弁である。 11 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 (since the circulating gas is ½ or less of the conventional one, a small ½ or less The size is sufficient) [oxygen air compression means]. In this embodiment, the oxygen air compressor 11 is a small oxygen air compressor (oilless centrifugal compressor: discharge pressure 5 kg / cm 2 G [0. An oxygen air compressor of about 5 MPaG (gauge pressure)] is used. The oxygen air compressor 11 has an oilless mechanism in order to prevent an explosion when the compressed air X containing high-concentration oxygen is further compressed. 11 a is a second feed pipe that feeds the high concentration oxygen-containing compressed air Y that has passed through the oxygen air compressor 11 to the second adsorption towers 12 and 13. Nos. 12 and 13 are filled with an adsorbent such as commercially available molecular sieves, and a pair of small second adsorption towers that alternately adsorb and regenerate (the size is smaller than 1/2 the conventional one). and a is) and water traces remaining oxygen air compressor hyperoxia-containing compressed air Y which is further compressed by 11, carbon dioxide, the effect of adsorbing and removing C n M m and NO X, and the like. Reference numeral 14 denotes a second discharge pipe which discharges waste gas that has been regenerated in the second adsorption towers 12 and 13 to the atmosphere. The system composed of the second adsorption towers 12 and 13 and the pipe passages with the on-off valves 16a, 16b, 19a and 19b is TSA. In the figure, 16a, 16b, 17a, 17b, 18a, 18b, 19a, 19b are on-off valves for alternately adsorbing and regenerating the second adsorption towers 12, 13.
２１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１２，１３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２１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２１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、１／２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が底部に溜まり、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２８下部の凝縮器（コンデンサー）３０に導入され、残部が窒素ガス取出パイプ２６を経由し膨脹タービン３７の駆動ガスとなる。そして、凝縮器３０に導入された窒素ガスは、そこで液化されて液体窒素となり、第２還流用パイプ３２を経て高圧精留塔２３の上部に還流液として戻り、高圧精留塔２３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と向流的に接触し、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２４はさらに酸素リッチになり、低沸点成分ガス（窒素ガス）は高圧精留塔２３の上部に向かって上昇する。窒素ガス取出パイプ２６から取出された窒素ガスは、主熱交換器２１に送られ、この主熱交換器２１を通過する圧縮空気を冷却したのち、第１連結パイプ２６ａを経由して膨脹タービン３７に供給され、先に述べたように、膨脹タービン３７の駆動源となり寒冷を発生する。３８は開閉弁３８ａ付き迂回路である。すなわち、窒素ガス取出パイプ２６，開閉弁２６ｂ付き第１連結パイプ２６ａを経て膨脹タービン３７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っ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３７ａを経由して主熱交換器２１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３７ｂを経由して放出され、一部が分岐パイプ４０を経由して第２吸着塔１２，１３の吸着剤の再生ガスとなる。この分岐パイプ４０は、導入された窒素ガスを、ヒータ４１を有する第１パイプ４２もしくは、ヒータなしの第２パイプ４３に供給する作用をする。４４は第３パイプであり、第１パイプ４２もしくは第２パイプ４３を経た窒素ガスを第２吸着塔１２，１３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 and the like, and the high-concentration oxygen-containing compressed air Y from which a small amount of water, carbon dioxide and the like are adsorbed and removed by the second adsorption towers 12 and 13 is cooled to an ultra-low temperature. . The main heat exchanger 21 also has a small flow size of about ½ or less because the amount of the circulation gas is ½ that of the conventional heat exchanger 21. Reference numeral 22 denotes a supply pipe for feeding the high-concentration oxygen-containing compressed air Y cooled to an ultra-low temperature by the main heat exchanger 21 into the lower portion of the high-pressure rectification tower 23. This high-pressure rectification tower (shelf type or packed column type) 23 also has a capacity of 1/2 or less because the flowing gas is 1/2 or less of the conventional gas, and has a size of 1/2 or less. . Inside the high-pressure rectification tower 23, of the high-concentration oxygen-containing compressed air Y sent from the supply pipe 22, the liquid high-concentration oxygen-containing liquid air 24 accumulates at the bottom, and the nitrogen gas rises upward. A part of the nitrogen gas rising to the upper part is introduced into the condenser (condenser) 30 at the lower part of the low-pressure rectification tower 28 via the first reflux pipe 31, and the remaining part is expanded via the nitrogen gas extraction pipe 26. It becomes a driving gas for the turbine 37. The nitrogen gas introduced into the condenser 30 is liquefied there to become liquid nitrogen, returns to the upper portion of the high pressure rectification column 23 via the second reflux pipe 32, and returns to the lower portion of the high pressure rectification column 23. The high-boiling component gas (oxygen gas) of the high-concentration oxygen-containing compressed air Y is liquefied and flowed down in contact with the high-concentration oxygen-containing compressed air Y ascending from below. For this reason, the liquid high-concentration oxygen-containing liquid air 24 that accumulates at the bottom becomes further 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, the expansion turbine 37 is passed through the first connection pipe 26a. As described above, it serves as a drive source for the expansion turbine 37 and generates cold. Reference numeral 38 denotes a bypass with an on-off valve 38a. That is, the nitrogen gas introduced into the expansion turbine 37 through the nitrogen gas extraction pipe 26 and the first connection pipe 26a with the on-off valve 26b expands inside and becomes extremely low in temperature by performing thermodynamic external work. The necessary amount of cold is generated and enters the main heat exchanger 21 via the second connecting pipe 37a in that state, where heat is exchanged with the raw air to give the generated cold to the raw air. The room temperature is reached, most of which is discharged as waste gas via the discharge pipe 37 b, and part of it becomes the regeneration gas for the adsorbent in the second adsorption towers 12 and 13 via the branch pipe 40. The branch pipe 40 serves to supply the introduced nitrogen gas to the first pipe 42 having the heater 41 or the second pipe 43 without the heater. Reference numeral 44 denotes a third pipe, which functions to supply nitrogen gas that has passed through the first pipe 42 or the second pipe 43 to the second adsorption towers 12 and 13 as adsorbent regeneration gas.
２８は高圧精留塔２３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２３の底部に溜まる液体の高濃度酸素含有液体空気２４が膨脹弁２９ａ付き送給パイプ２９を経て送り込まれる。この低圧精留塔２８には、その底部に凝縮器３０が設けられており、そこに、高圧精留塔２３から取り出された窒素ガスの一部が第１還流用パイプ３１を介して導入される。この窒素ガスは、低圧精留塔２８の底部に溜まる液体酸素（ＬＯ2：純度９９．７体積％程度）３４を加温して液体酸素３４を気化させる働きをし、それ自身は液体酸素３４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３２ａ付き第２還流用パイプ３２を通って高圧精留塔２３の上部に還流し還流液となる。また、上記液体窒素３４の残部は、流量調整弁３３ａ付き分岐パイプ３３を通って低圧精留塔２８の上部に導入され還流液となって低圧精留塔２８内を流下し気液分離作用をする。３５は低圧精留塔２８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２８の底部に溜まる液体酸素３４から気化した高純度の酸素ガスを取り出して主熱交換器２１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。３６は低圧精留塔２８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２８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２１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、３９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、吸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 column (a shelf type or packed column type) provided above the high-pressure rectification column 23, and a liquid high-concentration oxygen-containing liquid air 24 collected at the bottom of the high-pressure rectification column 23 is an expansion valve. It is fed through a feeding pipe 29 with 29a. The low-pressure rectification column 28 is provided with a condenser 30 at the bottom thereof, and a part of the nitrogen gas taken out from the high-pressure rectification column 23 is introduced through the first reflux pipe 31. The This nitrogen gas serves to heat liquid oxygen 34 (LO 2 : purity of about 99.7% by volume) 34 accumulated at the bottom of the low-pressure rectification column 28 to vaporize the liquid oxygen 34 itself. As described above, a part of the liquid is refrigerated to the upper part of the high-pressure rectification column 23 through the second reflux pipe 32 with the flow rate adjusting valve 32a to become a reflux liquid. The remaining portion of the liquid nitrogen 34 is introduced into the upper portion of the low-pressure rectification column 28 through the branch pipe 33 with the flow rate adjusting valve 33a and flows down in the low-pressure rectification column 28 to perform the gas-liquid separation action. To do. 35 is a product oxygen gas take-out pipe extending from the lower side of the low-pressure rectification column 28, and the high-purity oxygen gas evaporated from the liquid oxygen 34 accumulated at the bottom of the low-pressure rectification column 28 is taken out into the main heat exchanger 21. It is guided and heat-exchanged with the compressed air Y containing high-concentration oxygen to bring it to room temperature, and sends it out as a product oxygen gas. 36 is a product nitrogen gas extraction pipe extending from the upper part of the low-pressure rectification column 28. The nitrogen gas rising to the upper part of the low-pressure rectification column 28 is taken out and sent to the main heat exchanger 21, and compressed air Y containing high-concentration oxygen In addition to cooling, the temperature of itself is raised to room temperature and the product nitrogen gas is sent out of the apparatus. In the figure, reference numeral 39 denotes a cold box, which is filled with a heat insulating material (not shown) such as pearlite used for low temperature heat insulation. In this embodiment, the lines of the first adsorption towers 2 and 3 concentrate oxygen by nitrogen gas adsorption. However, an oxygen adsorbed and concentrated by an adsorbent that adsorbs oxygen gas is used. You may make it take out gas.
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，水分，炭酸ガスおよび炭化水素ガス（ＣnＨm）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、本発明の最大の特徴である。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）１１に導入し、この酸素空気圧縮機１１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吸着塔１２，１３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ＮＯX等を吸着除去する。つぎに、水，炭酸ガスおよびＮＯX等が吸着除去された高濃度酸素含有圧縮空気Ｙを主熱交換器２１内に送り込んで超低温に冷却し、その状態で高圧精留塔２３の下部に導入する。ついで、高圧精留塔２３内で、この高濃度酸素含有圧縮空気Ｙと、低圧精留塔２８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−１８３℃，同じく窒素の沸点−１９６℃）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２６から取り出して主熱交換器２１に送り込んだのち、膨脹タービン３７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１２，１３の再生ガスとする。 Using this apparatus, nitrogen gas and oxygen gas can be produced as follows. That is, first, external air is taken in from the air compressor (air compression means) 1, where the air is compressed at a low pressure, and moisture in the compressed air is removed by a water separator (not shown). In this state, it is sent to the first adsorption towers (oxygen concentrating means) 2 and 3 to adsorb and remove nitrogen gas, moisture, carbon dioxide gas, hydrocarbon gas (C n H m ) and the like in the compressed air. Thereby, the oxygen gas in compressed air is concentrated. This is the greatest feature of the present invention. Next, 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. After compression and high-concentration oxygen-containing compressed air Y, the compressed air Y is sent to the second adsorption towers 12 and 13 to adsorb and remove water, carbon dioxide gas, NO x and the like in the high-concentration oxygen-containing compressed air Y. Next, the high-concentration oxygen-containing compressed air Y from which water, carbon dioxide gas, NO x and the like are adsorbed and removed is sent into the main heat exchanger 21 and cooled to an ultra-low temperature, and introduced into the lower portion of the high-pressure rectification column 23 in that state. To do. Next, in the high-pressure rectification column 23, the compressed air is rectified by bringing the high-concentration oxygen-containing compressed air Y and the reflux liquid produced in the low-pressure rectification column 28 into countercurrent contact, and the boiling points of nitrogen and oxygen (The boiling point of oxygen at atmospheric pressure −183 ° C. and the boiling point of nitrogen −196 ° C.), oxygen, which is a high-boiling component, in compressed air Y containing high-concentration oxygen is liquefied and nitrogen is used as a gas. The nitrogen gas is taken out from the nitrogen gas take-out pipe 26 and sent to the main heat exchanger 21, and then supplied to the expansion turbine 37. After generating cold here, most of the nitrogen gas is discharged outside the apparatus, and partly Is a regeneration gas for the second adsorption towers 12 and 13.
また、低圧精留塔２８の上部に溜まった窒素ガスを製品窒素ガス取出パイプ３６から取り出して主熱交換器２１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２３の底部に溜った液体の高濃度酸素含有液体空気２４を送給パイプ２９を経て低圧精留塔２８に送り込み、窒素を気化除去した液体酸素３４として低圧精留塔２８の底部に溜め、低圧精留塔２８底部の凝縮器３０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３５から取り出して主熱交換器２１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。 Further, the nitrogen gas accumulated in the upper portion of the low-pressure rectification column 28 is taken out from the product nitrogen gas take-out pipe 36 and sent to the main heat exchanger 21. After the temperature is raised to near room temperature, it is sent out as the product nitrogen gas to the outside of the apparatus. On the other hand, liquid air 24 containing high-concentration oxygen contained in the liquid at the bottom of the high-pressure rectification column 23 is sent to the low-pressure rectification column 28 via the feed pipe 29, and the low-pressure rectification column 28 is obtained as liquid oxygen 34 by vaporizing and removing nitrogen. Is vaporized by exchanging heat with nitrogen gas passing through the condenser 30 at the bottom of the low-pressure rectification column 28. The vaporized oxygen gas is taken out from the product oxygen gas take-out pipe 35, sent to the main heat exchanger 21, and heated to near room temperature, and then sent out as a product oxygen gas outside the apparatus. In this way, product oxygen gas and nitrogen gas are obtained.
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２０．９体積％から５０体積％程度に濃縮されているため、１０，０００ｍ3／ｈ（Ｎｏｒｍａｌ）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９７％とすると、理論上では、空気量＝（１０，０００÷０．５００）÷０．９７で算出され、約２０，６００ｍ3／ｈ（Ｎｏｒｍａｌ）の空気量であり、冒頭で述べた従来のものの４１％程度に減少している。しかも、１０，０００ｍ3／ｈ（Ｎｏｒｍａｌ）の酸素ガスを製造するのに必要な酸素空気圧縮機１１の圧縮動力が２０００ｋＷ程度にまで減少し、また、酸素空気圧縮機１の圧縮動力が３００ｋＷ程度に、真空ポンプ４の駆動動力が９００ｋＷ程度に、電気ヒータ４１の電力量が２００ｋＷ程度になると推測されるため、合計３４００ｋＷとなり、従来の７０％程度に減少している。したがって、３０％以上の省エネルギーを実現できる。 In the above embodiment, since the concentration of oxygen gas in the compressed air is concentrated from 20.9 vol% to about 50 vol% by the first adsorption towers 2 and 3 , 10,000 m 3 / h (Normal) The amount of air required to produce the oxygen gas is theoretically calculated as air amount = (10,000 ÷ 0.500) ÷ 0.97, assuming that the recovery efficiency of oxygen gas is 97%. The amount of air is 20,600 m 3 / h (Normal), which is reduced to about 41% of the conventional one described at the beginning. In addition, the compression power of the oxygen air compressor 11 necessary for producing 10,000 m 3 / h (normal) oxygen gas is reduced to about 2000 kW, and the compression power of the oxygen air compressor 1 is about 300 kW. Furthermore, since it is estimated that the driving power of the vacuum pump 4 is about 900 kW and the electric energy of the electric heater 41 is about 200 kW, the total is 3400 kW, which is about 70% of the conventional value. 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１１，主熱交換器２１を経由して高圧精留塔２３，低圧精留塔２８に供給している。そのため、酸素空気圧縮機１１以降の、主熱交換器２１，両精留塔２３，２８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い小形化を達成することができる。 In this embodiment, following the air compressor 1 for compressing the raw air, the first adsorption towers 2 and 3 for concentrating the oxygen gas in the compressed air are provided to increase the oxygen concentration in the raw air, This is supplied to the high pressure rectification column 23 and the low pressure rectification column 28 via the oxygen air compressor 11 and the main heat exchanger 21. Therefore, by realizing a significant reduction in the flow rate of each device such as the main heat exchanger 21 and the rectifying towers 23 and 28 after the oxygen air compressor 11, they can be reduced to less than half of the conventional one. As a result, a significant downsizing of the entire apparatus can be achieved.
例えば、７０，０００ｍ3／ｈ（Ｎｏｒｍａｌ）の酸素ガスを製造する場合、従来のものでは高圧精留塔２３の直径が７ｍ（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から、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４．２ｍ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 oxygen gas of 70,000 m 3 / h (Normal), the diameter of the high-pressure rectification column 23 is 7 m (our calculated value) in the conventional one, which is assembled at the factory and transported to the site. Since there was no means of transport, it had to be assembled locally, but in this embodiment, when producing the same amount of oxygen, the gas flowing through the rectification column would be ½ or less. The diameter of the rectification column can be about 4.2 m. Therefore, it is possible to assemble at the factory and transport it to the site, which enables significant labor savings.
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１２，１３を省いている。すなわち、第２吸着塔１２，１３，第２放出パイプ１４，開閉弁１６ａ，１６ｂ，１７ａ，１７ｂ，１８ａ，１８ｂ，１９ａ，１９ｂ付きのパイプ路，分岐パイプ４０および第１〜第３パイプ４２〜４４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, 13, the second discharge pipe 14, the on-off valves 16a, 16b, 17a, 17b, 18a, 18b, 19a, 19b with the pipe path, the branch pipe 40, and the first to third pipes 42- 44 is omitted. Other parts are the same as those in the above embodiment, and the same reference numerals are given to the same parts. In this embodiment, by installing the apparatus in a place where clean air is used as the raw material air, the same effects as in the above-described embodiment can be obtained, and simplification and miniaturization of the apparatus can be achieved.
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３７に代えて、装置外からタンクローリー等で液体酸素（ＬＯ2）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、４７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２８の下部に導入する導入パイプであり、この導入パイプ４７から導入された液体酸素が低圧精留塔２８の底部に流下し、この底部に溜まる液体酸素３４に合流する。４８は低圧精留塔２８から延びる排出用パイプであり、低圧精留塔２８の棚段（またはパックドカラム）２８ａの上部に溜まる窒素ガス（廃ＧＮ2）を取り出して過冷却器４９に導入し、この過冷却器４９を経た廃窒素ガスを主熱交換器２１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４９は、その内部に、送給パイプ２９内の高濃度酸素含有液体空気２４、分岐パイプ３３内の液体窒素（還流液）、製品窒素ガス取出パイプ３６内の製品窒素ガスおよび排出用パイプ４８内の廃窒素ガスを通し、送給パイプ２９内の高濃度酸素含有液体空気２４を冷却する作用をする。５０は低圧精留塔２８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２８の底部に溜まる液体酸素を取り出して主熱交換器２１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３５に導入する作用をする。５１は製品窒素ガス取出パイプ３６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プ３６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。５２は製品酸素ガス取出パイプ３５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３５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５３に供給する作用をする。５４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５２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５５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２３の天井面と、この高圧精留塔２３の上方に設けた低圧精留塔２８の底面とを一体化し同一材で形成している。図において、３６ａは製品窒素ガス取出パイプ３６内を通る製品窒素ガスを排出用パイプ４８に送給するパイプである。３９Ａ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填され真空吸引されている。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。 FIG. 3 shows still another embodiment of the air separation device of the present invention. In this embodiment, in place of the expansion turbine 37 in the embodiment shown in FIG. 2, a liquid oxygen storage tank (not shown) to which liquid oxygen (LO 2 ) is supplied from outside the apparatus by a tank lorry or the like is used. The apparatus is substantially the same as that shown in FIG. 2 except that liquid oxygen is used as a cold source. In the figure, 47 is an introduction pipe for introducing liquid oxygen from the liquid oxygen storage tank into the lower part of the low-pressure rectification tower 28 as a cold source, and the liquid oxygen introduced from this introduction pipe 47 is the bottom of the low-pressure rectification tower 28. To the liquid oxygen 34 accumulated at the bottom. Reference numeral 48 denotes a discharge pipe extending from the low-pressure rectification column 28. Nitrogen gas (waste GN 2 ) accumulated at the upper part of the shelf (or packed column) 28a of the low-pressure rectification column 28 is taken out and introduced into the supercooler 49. The waste nitrogen gas that has passed through the supercooler 49 is guided into the main heat exchanger 21, and the compressed air Y containing high-concentration oxygen is cooled and then discharged to the outside. The supercooler 49 includes therein high-concentration oxygen-containing liquid air 24 in the supply pipe 29, liquid nitrogen (refluxing liquid) in the branch pipe 33, product nitrogen gas in the product nitrogen gas extraction pipe 36, and discharge. The waste nitrogen gas in the pipe 48 is passed, and the high concentration oxygen-containing liquid air 24 in the supply pipe 29 is cooled. Reference numeral 50 denotes a liquid oxygen extraction pipe extending from the bottom surface of the low pressure rectification column 28. The liquid oxygen collected at the bottom of the low pressure rectification column 28 is taken out and guided into the main heat exchanger 21, and compressed air Y containing high concentration oxygen is supplied. While cooling, it raises itself to normal temperature and introduce | transduces into the product oxygen gas extraction pipe 35 as product oxygen gas. A product nitrogen gas compressor 51 is provided in the product nitrogen gas take-out pipe 36, and works to increase the product nitrogen gas passing through the product nitrogen gas take-out pipe 36 to a predetermined pressure. Reference numeral 52 denotes a first product oxygen gas compressor provided in the product oxygen gas take-out pipe 35. The product oxygen gas passing through the product oxygen gas take-out pipe 35 is boosted to a predetermined pressure and supplied to the low-pressure product oxygen gas take-out pipe 53. Works. Reference numeral 54 denotes a second product oxygen gas compressor, which further increases the pressure of the product oxygen gas that has passed through the first product oxygen gas compressor 52 and supplies it to the high-pressure product oxygen gas extraction pipe 55. In this embodiment, the ceiling surface of the high pressure rectification column 23 and the bottom surface of the low pressure rectification column 28 provided above the high pressure rectification column 23 are integrally formed of the same material. In the figure, reference numeral 36 a denotes a pipe for supplying the product nitrogen gas passing through the product nitrogen gas extraction pipe 36 to the discharge pipe 48. Reference numeral 39A denotes a cold box, which is filled with a heat insulating material such as pearlite and vacuumed. The other parts are the same as those of the embodiment shown in FIG. 2, and the same reference numerals are given to the same parts.
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、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，水分，炭酸ガスおよび炭化水素ガス（ＣnＨm）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）１１に導入し、この酸素空気圧縮機１１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２１内に送り込んで超低温に冷却し、その状態で高圧精留塔２３の下部に導入する。ついで、高圧精留塔２３内で、この高濃度酸素含有圧縮空気Ｙと、低圧精留塔２８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−１８３℃，同じく窒素の沸点−１９６℃）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 from the air compressor (air compressing means) 1, compressed at a low pressure, and compressed by a water separator (not shown). Moisture in the air is removed and sent to the first adsorption tower (oxygen concentrating means) 2 and 3 in that state to adsorb nitrogen gas, moisture, carbon dioxide gas, hydrocarbon gas (C n H m ), etc. in the compressed air. Remove. Thereby, the oxygen gas in compressed air is concentrated. Next, 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. Compressed and compressed air Y containing high concentration oxygen. Next, this high-concentration oxygen-containing compressed air Y is sent into the main heat exchanger 21 and cooled to an ultra-low temperature, and introduced into the lower portion of the high-pressure rectification tower 23 in this state. Next, in the high-pressure rectification column 23, the compressed air is rectified by bringing the high-concentration oxygen-containing compressed air Y and the reflux liquid produced in the low-pressure rectification column 28 into countercurrent contact, and the boiling points of nitrogen and oxygen (The boiling point of oxygen at atmospheric pressure −183 ° C. and the boiling point of nitrogen −196 ° C.), oxygen, which is a high-boiling component, in compressed air Y containing high-concentration oxygen is liquefied and nitrogen is used as a gas.
また、低圧精留塔２８の上部に溜まった窒素ガスを製品窒素ガス取出パイプ３６から取り出して過冷却器（熱交換器）４９に送り込み、主熱交換器２１に導入して主熱交換器２１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２３の底部に溜った高濃度酸素含有液体空気２４を送給パイプ２９で過冷却器４９に送り込み、ここで冷却した気−液混合状態の高濃度酸素含有液体空気２４を低圧精留塔２８に送り込み、窒素を気化除去した液体酸素３４として低圧精留塔２８の底部に溜め、低圧精留塔２８底部の凝縮器３０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３５から取り出して主熱交換器２１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５２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５３により装置外に送り出し、第２製品酸素圧縮機５４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５５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。 Further, the nitrogen gas accumulated in the upper portion of the low-pressure rectification column 28 is taken out from the product nitrogen gas take-out pipe 36, sent to a supercooler (heat exchanger) 49, introduced into the main heat exchanger 21, and introduced into the main heat exchanger 21. After raising the temperature to near normal temperature, it is sent out as a 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 by the feed pipe 29, and the high-concentration oxygen-containing liquid air 24 in the gas-liquid mixed state cooled here is It is sent to the low-pressure rectification column 28 and is stored at the bottom of the low-pressure rectification column 28 as liquid oxygen 34 from which nitrogen has been vaporized and removed, and is vaporized by heat exchange with nitrogen gas passing through the condenser 30 at the bottom of the low-pressure rectification column 28. The vaporized oxygen gas is taken out from the product oxygen gas take-out pipe 35 and sent to the main heat exchanger 21. After the temperature is raised to near room temperature, the product oxygen gas passed through the first product oxygen compressor 52 is reduced to low pressure product oxygen gas. The product oxygen gas is sent out of the apparatus by the take-out pipe 53, and the product oxygen gas passing through the second product oxygen compressor 54 is sent out of the apparatus by the high-pressure product oxygen gas take-out 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・効果を奏する。 As described above, this embodiment also provides the same operations and effects as 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、膨脹タービン３７に代えて、装置外からタンクローリー等で液体窒素（ＬＮ2）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、４７ａ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２３の上部に導入する導入パイプであり、この導入パイプ４７ａから導入された液体窒素と低圧精留塔２８下部の凝縮器３０で液化された液体窒素の一部とが、高圧精留塔２３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 place of the expansion turbine 37 in the embodiment shown in FIG. 2, a liquid nitrogen storage tank (not shown) to which liquid nitrogen (LN 2 ) is supplied from outside the apparatus by a tank lorry or the like is used. The apparatus is substantially the same as that shown in FIG. 2 except that liquid nitrogen is used as a cold source. That is, 47a is an introduction pipe for introducing liquid nitrogen from the liquid nitrogen storage tank into the upper part of the high pressure rectification tower 23 as a cold source, and the liquid nitrogen introduced from the introduction pipe 47a and the condensation of the lower part of the low pressure rectification tower 28 are condensed. Part of the liquid nitrogen liquefied by the vessel 30 is introduced into the upper portion of the high pressure rectification column 23. The other parts are the same as those of the embodiment shown in FIG. 2, and the same reference numerals are given to the same parts.
図５は本発明の空気分離装置の参考形態を示している。この参考形態では、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１ａ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１１に導入する導入パイプ５７（図１には、符号５７を付していない）とを、開閉弁（もしくは流量調整弁）５８ａ付き連通パイプ５８で連通している。そして、上記開閉弁５８ａ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５８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５７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５７に送り込み、この導入パイプ５７で両者を合流させて、連通パイプ５８を介して導入パイプ５７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５７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。この参考形態では、高圧精留塔２３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。 FIG. 5 shows a reference embodiment of the air separation device of the present invention. In this reference embodiment, in the embodiment shown in FIG. 1, a first feed pipe 1a for feeding compressed air through the air compressor 1 to the first adsorption tower 2, the first adsorption tower 2 An introduced pipe 57 (not denoted by reference numeral 57 in FIG. 1) for introducing the high-concentrated oxygen-containing compressed air X into the oxygen-air compressor 11 is connected to a communication pipe 58 with an on-off valve (or flow rate adjusting valve) 58a. It communicates with. 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 adsorption tower 2, 3) and the remaining portion is fed to the introduction pipe 57 via the first adsorption towers 2 and 3, and the introduction pipe 57 joins the two through the communication pipe 58. A part of the compressed air introduced into the introduction pipe 57 is diluted with the remaining oxygen gas concentration of the compressed air introduced into the introduction pipe 57 via the first adsorption towers 2 and 3. Other parts are the same as those in the embodiment shown in FIG. 1, and the same reference numerals are given to the same parts. In this reference embodiment, the concentration of oxygen gas in the compressed air supplied to the bottom of high pressure column 23 is lowered, it is possible to reduce the product oxygen gas amount. Therefore, when it is desired to reduce the amount of product oxygen gas, this can be dealt with .
１ 空気圧縮機
２，３ 第１吸着塔
１１ 酸素空気圧縮機
１２，１３ 第２吸着塔
２１ 主熱交換器
２３ 高圧精留塔
２８ 低圧精留塔
DESCRIPTION OF SYMBOLS 1 Air compressor 2, 3 1st adsorption tower 11 Oxygen air compressor 12, 13 2nd adsorption tower 21 Main heat exchanger 23 High pressure rectification tower 28 Low pressure rectification tower
Claims (5)
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| Application Number | Priority Date | Filing Date | Title |
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| JP2004002877A JP4782380B2 (en) | 2003-03-26 | 2004-01-08 | Air separation device |
| US10/550,627 US20060272352A1 (en) | 2003-03-26 | 2004-03-25 | Air separator |
| KR1020057017678A KR101099855B1 (en) | 2003-03-26 | 2004-03-25 | Air separator |
| BRPI0408715-1A BRPI0408715A (en) | 2003-03-26 | 2004-03-25 | air separator |
| EP04723340.8A EP1612496B1 (en) | 2003-03-26 | 2004-03-25 | Air separator |
| CNB2004800080462A CN100390481C (en) | 2003-03-26 | 2004-03-25 | Air separator |
| PCT/JP2004/004145 WO2004085941A1 (en) | 2003-03-26 | 2004-03-25 | Air separator |
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| JP2003086052 | 2003-03-26 | ||
| JP2004002877A JP4782380B2 (en) | 2003-03-26 | 2004-01-08 | Air separation device |
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| JP4782380B2 true JP4782380B2 (en) | 2011-09-28 |
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| US (1) | US20060272352A1 (en) |
| EP (1) | EP1612496B1 (en) |
| JP (1) | JP4782380B2 (en) |
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| JP5005894B2 (en) | 2005-06-23 | 2012-08-22 | エア・ウォーター株式会社 | Nitrogen generation method and apparatus used therefor |
| FR2911391A1 (en) * | 2007-01-16 | 2008-07-18 | Air Liquide | Cryogenic separation method for gas, involves using distillation columns and absorption column with heat and/or material exchange section between descending liquid and mounting gas, where section has specific parameter |
| KR100930316B1 (en) * | 2008-05-16 | 2009-12-08 | 대성산업가스 주식회사 | Ultra-small liquid nitrogen and liquid oxygen production device |
| JP2013212474A (en) * | 2012-04-03 | 2013-10-17 | Jfe Engineering Corp | Gas separation apparatus |
| JP5529211B2 (en) * | 2012-06-19 | 2014-06-25 | 東京瓦斯株式会社 | Gas separator |
| KR101644245B1 (en) * | 2014-11-13 | 2016-08-11 | 참좋은우리 주식회사 | Ozone cream is manufactured by the manufacturing apparatus with a humidity adjusting device |
| KR101644244B1 (en) * | 2014-11-13 | 2016-08-11 | 참좋은우리 주식회사 | Manufacturing methods take advantage of Ozone cream manufacturing equipment with humidity-conditioned |
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| WO2024010756A1 (en) * | 2022-07-08 | 2024-01-11 | Entegris, Inc. | Methods and equipment for cryogenic removal of impurities from oxygen gas |
| CN115451655B (en) * | 2022-09-29 | 2023-04-28 | 北京飞燕石化环保科技发展有限公司 | Air separation device |
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-
2004
- 2004-01-08 JP JP2004002877A patent/JP4782380B2/en not_active Expired - Fee Related
- 2004-03-25 CN CNB2004800080462A patent/CN100390481C/en not_active Expired - Fee Related
- 2004-03-25 WO PCT/JP2004/004145 patent/WO2004085941A1/en active Application Filing
- 2004-03-25 EP EP04723340.8A patent/EP1612496B1/en not_active Revoked
- 2004-03-25 KR KR1020057017678A patent/KR101099855B1/en active IP Right Grant
- 2004-03-25 US US10/550,627 patent/US20060272352A1/en not_active Abandoned
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Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0408715A (en) | 2006-03-07 |
| CN100390481C (en) | 2008-05-28 |
| KR101099855B1 (en) | 2011-12-28 |
| EP1612496B1 (en) | 2016-12-07 |
| EP1612496A1 (en) | 2006-01-04 |
| CN1764813A (en) | 2006-04-26 |
| US20060272352A1 (en) | 2006-12-07 |
| WO2004085941A1 (en) | 2004-10-07 |
| JP2004309119A (en) | 2004-11-04 |
| KR20060024352A (en) | 2006-03-16 |
| EP1612496A4 (en) | 2012-08-29 |
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