JP4594360B2 - 深冷空気液化分離装置およびその運転方法 - Google Patents
深冷空気液化分離装置およびその運転方法 Download PDFInfo
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- JP4594360B2 JP4594360B2 JP2007220015A JP2007220015A JP4594360B2 JP 4594360 B2 JP4594360 B2 JP 4594360B2 JP 2007220015 A JP2007220015 A JP 2007220015A JP 2007220015 A JP2007220015 A JP 2007220015A JP 4594360 B2 JP4594360 B2 JP 4594360B2
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- 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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- F25J3/0429—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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- 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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- 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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- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
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- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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Description
(2)ガス製造運転中の液化熱交換器のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されている。従って、温端側がマイナスの温度になっているということがなく、液製造運転への切換え時に低温流体が低温のまま放出されることがないため、常温ラインの配管が損傷するという危険性がない。
(3)液化熱交換器は収縮と膨張とを繰り返すことがないため、液化熱交換器の耐久寿命が向上する。
なお、水分・炭酸ガスを除去するために、例えば第1吸着塔3b1に原料空気が導入されている間に、第2吸着塔3b2の吸着剤を再生するために、この第2吸着塔3b2には、図示しないヒータで加熱したパージガスが供給され、水分・炭酸ガスを吸着した吸着剤が再生されるように構成されている。
そして、前記高圧膨張タービン12の膨張機12bの出口は、第5空気導入ライン14を介して前記空気供給先ライン5の前記第2空気導入ライン8の連通部と下部塔15bとの間に連通している。そのため、液化熱交換器7で約−100℃に冷却された原料空気が前記第4空気導入ライン13から導入されると、前記膨張機12bで約0.45MPaGまで膨張されて寒冷を発生した原料空気が第5空気導入ライン14を介して下部塔15bに導入される。なお、前記第1開閉弁V1、第2開閉弁V2、第3開閉弁V3、第4開閉弁V4、入側開閉弁9a、および出側開閉弁10aは、ガス製造運転と、液製造運転の切換えに際して、遠隔操作により開閉操作される自動開閉弁である。
即ち、原料空気圧縮機2で圧縮されて約90℃に昇温した原料空気が予冷ユニット3aで10〜40℃に予冷されると共に、予冷された原料空気が吸着塔ユニット3bに導入され、水分・炭酸ガスが除去されて精製される。そして、精製された原料空気の一部が主熱交換器4に導入され、液化点付近の温度になるまで冷却されて空気供給先ライン5を介して複式精留塔15に供給される。また、これと並行して、吸着塔ユニット3aで精製された原料空気の残りが第1空気導入ライン6(第1開閉弁V1開弁)から液化熱交換器7に導入され、液化点付近の温度になるまで冷却されて第2空気導入ライン8(第2開閉弁V2開弁)から空気供給先ライン5に合流し、前記主熱交換器4から出た原料空気の一部と共に複式精留塔15の下部塔15bに導入される。
即ち、吸着塔ユニット3bで精製された原料空気は2分され、2分された原料空気の一部が主熱交換器4に導入されて、液化点付近の温度になるまで冷却される。主熱交換器4から出た原料空気の一部は、空気供給先ライン5から複式精留塔15の下部塔15bに導入される。原料空気の残りは、空気導入元ライン9(第1開閉弁V1閉弁、入側開閉弁9a開弁)を介して昇圧圧縮機9bに導入され、約3.0MPaGまで昇圧される。昇圧された原料空気の残りは2分され、2分された原料空気の残りの1部は、液化熱交換器7で液化され、液体製品を製造するための寒冷源として空気導入先ライン10(出側開閉弁10a開弁)から複式精留塔15の下部塔15bに導入される。
膨張機12bに導入された、2分された原料空気の残りの残りは、約0.45MPaGに膨張されて深冷空気液化分離装置1の液製造運転のための寒冷を発生した後、空気供給先ライン5に合流し、前記主熱交換器4から出た2分された原料空気の一部と共に複式精留塔15の下部塔15bに導入される。
(2)ガス製造運転中の液化熱交換器のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されている。従って、温端側がマイナスの温度になっているということがなく、液製造運転への切換え時に低温流体が低温のまま放出されることがないため、常温ラインの配管が損傷するという危険性がない。
(3)液化熱交換器7は収縮と膨張とを繰り返すことがないため、液化熱交換器の耐久寿命が向上する。
2…原料空気圧縮機
3…空気供給元ライン,3a…予冷ユニット,
3b…吸着塔ユニット,3b1…第1吸着塔,3b2…第2吸着塔
4…主熱交換器
5…空気供給先ライン
6…第1空気導入ライン
7…液化熱交換器,7a…熱交換流
8…第2空気導入ライン
9…空気導入元ライン,9a…入側開閉弁,9b…昇圧圧縮機
10…空気導入先ライン,10a…出側開閉弁
11…第3空気導入ライン
12…高圧膨張タービン,12a…圧縮機,12b…膨張機
13…第4空気導入ライン
14…第5空気導入ライン
15…複式精留塔,15a…上部塔,15b…下部塔,15c…アルゴン精製装置
16…液体窒素供給ライン
17…液体酸素供給ライン
18…窒素ガス供給ライン,18a…廃ガス排出ライン
19…酸素ガス供給ライン
20…第1空気分流ライン
21…第2空気分流ライン
22…低圧膨張タービン,22a…圧縮機,22b…膨張機
Claims (2)
- 窒素ガス、酸素ガスを製造するガス製造運転と、窒素ガス、酸素ガス並びに液体窒素及び/又は液体酸素を製造する液製造運転とに切換え操作される深冷空気液化分離装置において、
原料空気圧縮機と、この原料空気圧縮機で圧縮された原料空気を予冷する予冷ユニットと、この予冷ユニットで予冷された原料空気から水分・炭酸ガスを除去して精製する吸着塔ユニットと、製品として生成される窒素ガス、酸素ガスが冷却媒体として導入され、前記吸着塔ユニットで精製された原料空気の一部を冷却する主熱交換器と、前記吸着塔ユニットで精製された原料空気の残りを前記液製造運転時に圧縮する昇圧圧縮機と、前記窒素ガスの生成に伴い生成する廃ガスが冷却媒体として導入され、前記昇圧圧縮機で昇圧された原料空気の一部を冷却する液化熱交換器と、前記昇圧圧縮機で圧縮された原料空気の残りの一部を膨張させて寒冷を発生させる高圧膨張タービンと、前記主熱交換器からの原料空気と前記液化熱交換器からの原料空気とが導入され、該原料空気を窒素、酸素に精留分離する複式精留塔と、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第1開閉弁が介装され、前記吸着塔ユニットで精製された原料空気の残りを前記液化熱交換器に導入する第1空気導入ラインと、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第2開閉弁が介装され、前記液化熱交換器から出た原料空気を前記複式精留塔に導入する第2空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第3開閉弁が介装され、前記高圧膨張タービンの圧縮機側から出た原料空気を前記液化熱交換器に導入する第3空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第4開閉弁が介装され、前記液化熱交換器から出た原料空気を前記高圧膨張タービンの膨張機側に導入する第4空気導入ラインと、前記液製造運転に際して前記第4空気導入ラインから導入され、前記高圧膨張タービンの膨張機で膨張されて寒冷を発生した原料空気を前記複式精留塔に導入する第5空気導入ラインと、を備えたことを特徴とする深冷空気液化分離装置。 - 原料空気を原料空気圧縮機で圧縮し、前記原料空気圧縮機から出た原料空気を予冷ユニットで予冷し、予冷した原料空気を水分・炭酸ガスを除去する吸着塔ユニットに導入し、この吸着塔ユニットから出た原料空気の一部を主熱交換器に導入して、複式精留塔からの製品として生成される窒素ガス、酸素ガスとの熱交換によって冷却する一方、残りの原料空気を液化熱交換器に導入して前記複式精留塔からの廃ガスとの熱交換によって冷却し、前記主熱交換器から出た原料空気と前記液化熱交換器から出た原料空気とを前記複式精留塔に導入して窒素ガス、酸素ガスを製造するガス製造運転と、
前記吸着塔ユニットから出た原料空気の一部を前記主熱交換器に導入して、前記複式精留塔からの製品として生成される窒素ガス、酸素ガスとの熱交換によって冷却する一方、残りの原料空気を昇圧圧縮機で昇圧させた後に二分し、二分した一方の原料空気を前記液化熱交換器に導入して前記複式精留塔からの廃ガスとの熱交換によって冷却し、二分した他方の原料空気を高圧膨張タービンの圧縮機で圧縮して前記液化熱交換器に導入し、この液化熱交換器から出た原料空気を前記高圧膨張タービンの膨張機で膨張させた後に前記複式精留塔に導入すると共に、前記主熱交換器から出た原料空気、および前記液化熱交換器から出た前記二分した前記一方の原料空気を前記複式精留塔に導入して、窒素ガス、酸素ガス並びに液体窒素及び/又は液体酸素を製造する液製造運転とを、自動切換することを特徴とする深冷空気液化分離装置の運転方法。
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