JP7458226B2 - 空気分離装置及び酸素ガス製造方法 - Google Patents
空気分離装置及び酸素ガス製造方法 Download PDFInfo
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- 238000000926 separation method Methods 0.000 title claims description 60
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 title claims description 46
- 229910001882 dioxygen Inorganic materials 0.000 title claims description 46
- 238000004519 manufacturing process Methods 0.000 title claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 95
- 239000001301 oxygen Substances 0.000 claims description 95
- 229910052760 oxygen Inorganic materials 0.000 claims description 95
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 37
- 239000002994 raw material Substances 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 26
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 17
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 239000011552 falling film Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 2
- 239000012530 fluid Substances 0.000 description 15
- 239000007789 gas Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000001010 compromised effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000009795 derivation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- FAQJJMHZNSSFSM-UHFFFAOYSA-N phenylglyoxylic acid Chemical compound OC(=O)C(=O)C1=CC=CC=C1 FAQJJMHZNSSFSM-UHFFFAOYSA-N 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- 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
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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- 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
- F25J3/0429—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 feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- 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
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- F25J3/04406—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 dual pressure main column system
- F25J3/04412—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 dual pressure main column system in a classical double column flowsheet, 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
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- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid being air
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- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/50—One fluid being oxygen
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Description
[1] 原料空気を低温で蒸留し、少なくとも高圧窒素ガスと高圧酸素富化液化空気とに分離する高圧塔と、
少なくとも前記高圧酸素富化液化空気を低温で蒸留し、低圧窒素ガスと低圧液化酸素とに分離する低圧塔と、
前記高圧窒素ガスと前記低圧液化酸素とを間接的に熱交換し、前記高圧窒素ガスを液化して高圧液化窒素を生成し、前記低圧液化酸素を気化して低圧酸素ガスを生成する第1凝縮器と、
前記原料空気の一部をさらに昇圧する空気昇圧機と、
前記低圧塔から抜き出した前記低圧液化酸素の一部を昇圧する液化酸素ポンプと、
前記空気昇圧機で昇圧された昇圧原料空気と、前記液化酸素ポンプによって昇圧された高圧液化酸素とを間接的に熱交換し、前記昇圧原料空気を液化して昇圧液化原料空気を生成し、前記高圧液化酸素を気化して高圧酸素ガスを生成する主熱交換器と、
前記低圧塔から抜き出した前記低圧液化酸素の一部と、前記原料空気の一部とを間接的に熱交換し、前記原料空気を液化して原料液化空気を生成し、前記低圧液化酸素を気化して低圧酸素ガスを生成する第2凝縮器とを備える、空気分離装置。
[2] 前記第1凝縮器が、流下液膜式の凝縮器である、前項[1]に記載の空気分離装置。
[3] 前項[1]又は2に記載の空気分離装置を用いて、酸素ガスを製造する方法であって、
前記空気昇圧機及び前記液化酸素ポンプの少なくとも一方が停止している場合、前記低圧塔から抜き出した前記低圧液化酸素を前記第2凝縮器で気化させ、低圧酸素ガスとして供給する、酸素ガス製造方法。
また、経路を流れる流体は、1種類の気体(ガス)、2種以上の混合気体(ガス)、1種類の液体、2種以上の混合液体、及びこれらの混合流体を含む。
バルブは、開閉バルブ、減圧バルブ、流量調整バルブ等を含む。
図1は、本発明の一実施形態である空気分離装置の構成の一例を示す系統図である。
図1に示すように、本実施形態の空気分離装置50は、空気圧縮機1、空気予冷器2、空気精製器3、主熱交換器4、高圧塔5、低圧塔6、第1凝縮器7、気液分離器8、第2凝縮器9、過冷器10、液化酸素ポンプ11、空気昇圧機12、空気予冷器13、膨張タービン14、経路L1~L13、バルブV1~V4、及びコールドボックスCLを備える。
本実施形態の空気分離装置50は、通常運転時には経路L9より製品高圧酸素ガスを取り出し、空気昇圧機12及び液化酸素ポンプ11のいずれかが停止した場合には、経路L11より製品低圧酸素ガスを取り出すことが可能な装置である。
高圧塔5は、経路L1Aから供給される高圧の原料空気と、経路L2Aから供給される昇圧液化原料空気と、経路L5から供給される高圧液化窒素とを低温で蒸留して、高圧窒素ガスと高圧酸素富化液化空気とに分離する。この低温での蒸留により、高圧塔5の上部には高圧窒素ガスが濃縮され、高圧塔5の下部には高圧酸素富化液化空気が濃縮される。
低圧塔6は、経路L3から供給される流体と、経路L6から供給される流体と、経路L7から供給される流体と、経路L13から供給される流体を低温で蒸留して、低圧窒素ガスと低圧液化酸素とに分離する。この低温での蒸留により、低圧塔6の上部~頂部(塔頂部)には低圧窒素ガスが濃縮され、低圧塔6の下部~底部(塔底部)には低圧液化酸素が濃縮される。
以下、本実施形態の空気分離装置50の運転方法(空気分離方法)、すなわち、上述した空気分離装置50を用いる酸素ガスの製造方法の一例について、詳細に説明する。
以下、上述した空気分離装置50の回転機械が停止した際(回転機械停止時)の空気分離方法(酸素ガスの製造方法)について、説明する。
尚、上記以外の部分については、通常運転時と基本的に、同じである。
通常運転時、空気圧縮機101から経路L101に供給される原料空気量を100とする。経路L109により、低圧塔106の底部から導出され、液化酸素ポンプ111に導入される低圧液化酸素の量は、20とする。通常運転時、経路L101により高圧塔105の下部に導入されるガス状の原料空気量は、60である。
一方、液化酸素との熱交換によって液化し、経路L102により高圧塔105の中間部に導入される液化原料空気量は、30である。
また、経路L103により、低圧塔106の中間部に導入されるガス状の原料空気は、10となる。
この場合、経路109を流れる液化酸素を気化する必要はないので、通常運転時に経路L102により高圧塔105の中間部に導入されていた液化原料空気は、空気昇圧機112で昇圧される必要が無く、経路L101から、ガス状態で高圧塔105に導入されることになる。従って、高圧塔下部から導入される原料空気量は、90となる。つまり、高圧塔105における上昇ガス量(原料空気)は、最大90となる。
通常運転時、回転機械停止時において、高圧塔5に導入される原料空気の状態を説明する。通常運転時においては、高圧塔5に導入される原料空気の状態は、従来の空気分離装置60と同じである。
1・・・空気圧縮機
2・・・空気予冷器
3・・・空気精製器
4・・・主熱交換器
5・・・高圧塔
6・・・低圧塔
7・・・第1凝縮器
8・・・気液分離器
9・・・第2凝縮器
10・・・過冷器
11・・・液化酸素ポンプ
12・・・空気昇圧機
13・・・空気予冷器(空気昇圧機アフタークーラ)
14・・・膨張タービン
L1~L13・・・経路
V1~V4・・・バルブ
CL・・・コールドボックス
Claims (3)
- 原料空気を低温で蒸留し、少なくとも高圧窒素ガスと高圧酸素富化液化空気とに分離する高圧塔と、
少なくとも前記高圧酸素富化液化空気を低温で蒸留し、低圧窒素ガスと低圧液化酸素とに分離する低圧塔と、
前記高圧窒素ガスと前記低圧液化酸素とを間接的に熱交換し、前記高圧窒素ガスを液化して高圧液化窒素を生成し、前記低圧液化酸素を気化して低圧酸素ガスを生成する第1凝縮器と、
前記原料空気の一部をさらに昇圧する空気昇圧機と、
前記低圧塔から抜き出した前記低圧液化酸素の一部を昇圧する液化酸素ポンプと、
前記空気昇圧機で昇圧された昇圧原料空気と、前記液化酸素ポンプによって昇圧された高圧液化酸素とを間接的に熱交換し、前記昇圧原料空気を液化して昇圧液化原料空気を生成し、前記高圧液化酸素を気化して高圧酸素ガスを生成する主熱交換器と、
前記低圧塔から抜き出した前記低圧液化酸素の一部と、前記原料空気の一部とを間接的に熱交換し、前記原料空気を液化して原料液化空気を生成し、前記低圧液化酸素を気化して低圧酸素ガスを生成する第2凝縮器と、前記第2凝縮器を収容する気液分離器とを備え、
前記低圧塔から前記低圧液化酸素の一部を抜き出す経路として、前記空気昇圧機及び前記液化酸素ポンプが共に稼動しているときに、前記気液分離器を介することなく、前記低圧液化酸素の一部を前記液化酸素ポンプによって加圧した後に回収する経路と、前記空気昇圧機及び前記液化酸素ポンプの少なくとも一方が停止しているときに、前記低圧液化酸素の一部を前記気液分離器に導入した後に回収する経路とが、別々に設けられている、空気分離装置。 - 前記第1凝縮器が、流下液膜式の凝縮器である、請求項1に記載の空気分離装置。
- 請求項1又は2に記載の空気分離装置を用いて、酸素ガスを製造する方法であって、
前記空気昇圧機及び前記液化酸素ポンプの少なくとも一方が停止している場合、前記低圧塔から抜き出した前記低圧液化酸素を前記第2凝縮器で気化させ、低圧酸素ガスとして供給する、酸素ガス製造方法。
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