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JP3969874B2 - Air liquefaction separator - Google Patents
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JP3969874B2 - Air liquefaction separator - Google Patents

Air liquefaction separator Download PDF

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JP3969874B2
JP3969874B2 JP36705798A JP36705798A JP3969874B2 JP 3969874 B2 JP3969874 B2 JP 3969874B2 JP 36705798 A JP36705798 A JP 36705798A JP 36705798 A JP36705798 A JP 36705798A JP 3969874 B2 JP3969874 B2 JP 3969874B2
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air
heat exchanger
liquid oxygen
path
cold
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JP2000193366A (en
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亮 田
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Air Liquide Japan GK
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Air Liquide Japan GK
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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
    • F25J3/04763—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
    • F25J3/04818—Start-up of the process
    • 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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • 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
    • F25J3/04406—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
    • 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
    • F25J3/04763—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
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • 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
    • 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
    • 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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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

【０００１】
【発明の属する技術分野】
本発明は、空気を液化精留して酸素ガスを製造する空気液化分離装置に関するものである。
【０００２】
【従来の技術】
従来、この種の空気液化分離装置としては、図２に示すように、外部から取り入れた原料空気の圧縮を行う圧縮機１、圧縮された原料空気を冷却する冷却器３、二酸化炭素及び水等の不純物の吸着除去を行う除炭乾燥器５を設けて、原料空気を順に導き、その圧縮、冷却、除炭された原料空気を、主熱交換器７において、廃ガス等を利用して液化点付近まで冷却し、冷却された原料空気を導いて精留を行う精留塔を設けたものが知られている。このような場合、前記精留塔は、前記原料空気の予備精留を行う高圧精留塔１１及び空気の最終分離を行う低圧精留塔１２、高圧精留塔１１と低圧精留塔１２の間にあって低圧精留塔１２に対してはリボイラー、高圧精留塔１１に対してはコンデンサーの働きを行う主凝縮器部１９から構成されたものが利用される。また、前記精留塔に対する寒冷は、寒冷供給部１７を設けて、液体酸素を前記主凝縮器部１９に供給する構成としていた。
【０００３】
このような空気液化分離装置では、通常、前記寒冷供給部１７から液体酸素を前記主凝縮器部１９に直接導入して寒冷として用いる構成としていた。供給された液体酸素は、前記主凝縮器部１９との熱交換を行うとともに、製品酸素の原料として用いられる。
ここで、原料空気に含有される微量の炭化水素等の可燃性物質は、前記除炭乾燥器５である程度除去されるものの、除去しきられなかったものは前記精留塔９内部に導入されてしまう。すると、蒸気圧平衡等との関係から、前記低圧精留塔下部には、液体酸素と共に炭化水素等の可燃性物質が次第に濃縮されることになる。このような構成は、コスト面等から小型の空気液化分離装置によく用いられるが、濃縮される液体酸素中での前記可燃性物質の爆発等を回避するためにも、前記可燃性物質が濃縮される前記主凝縮器部１９の保安管理は極めて重大である。そのため、前記主凝縮器部１９の可燃性物質量が常に既定値以下になるように、前記主凝縮器部１９から液体酸素を少量パージする処置をとる必要があり、可燃性物質を含む液体酸素は、パージされた後、廃棄されていた。
【０００４】
またさらに、パージされるガスをそのまま廃棄する場合には、その冷熱も廃棄することになって不経済である。そこで、前記空気液化分離装置に熱交換器を設け、精留塔９内にある前記主凝縮器部１９からパージされる液体酸素を熱交換器１６に導く経路と、前記熱交換器１６により気化した酸素ガスを取り出す経路と、原料空気を前記熱交換器１６に導き、熱交換可能にする経路と、前記熱交換器１６において冷却された原料空気を精留塔９に導く経路を設け、前記主凝縮器部１９からパージされる液体酸素の保有する冷熱を回収可能な空気液化分離装置が提案されている。
【０００５】
【発明が解決しようとする課題】
しかし、そのような空気液化分離装置でも、寒冷供給部１７から寒冷として供給する液体酸素は、前記寒冷供給部１７から、直接、前記主凝縮器部１９に導入されていた。そのため、前記主凝縮器部１９の可燃性物量の増加を防止するために液体酸素をパージさせたとしても、前記主凝縮器部１９には、空気液化分離装置に寒冷を供給する寒冷供給部１７から寒冷として液体酸素が供給される。前記寒冷供給部１７中の液体酸素には微量ながらも不純物としての可燃性物質が含有されているので、前記主凝縮器部１９における可燃性物質量の増加を防止するためには、前記主凝縮器部１９からパージする液体酸素に留意するのみならず、前記寒冷供給部１７からの寒冷としての液体酸素中の可燃性物質にも留意する必要があった。つまり、前記主凝縮器部１９における可燃性物質量の増加を防止するためには、前記寒冷供給部１７からの寒冷としての液体酸素中の可燃性物質の双方を勘案して、前記低圧精留塔１２下部から液体酸素をパージさせる必要があり、改善の余地があった。
【０００６】
そこで、本発明の目的は、前記主凝縮器部１９における可燃性物質の蓄積を、前記寒冷供給部１７からの液体酸素中の可燃性物質含有量に影響されることなく抑えることができる空気液化分離装置を提供することにある。即ち、前記寒冷供給部１７からの液体酸素中の可燃性物質含有量に影響されることなく、前記主凝縮器部１９からの液体酸素のパージ量を設定できる空気液化分離装置を提供することにある。
【０００７】
【課題を解決するための手段】
前記目的を達成するための本発明空気液化分離装置の構成は、外部から取り入れた原料空気を主熱交換器で液化点付近まで冷却し、精留塔に導入する経路を有する空気液化分離装置において、原料空気の一部を前記主熱交換器を経由せずに冷却する熱交換器を設け、前記精留塔内の主凝縮器部から液体酸素をパージ可能、かつ、前記主凝縮器部に液体酸素を供給可能とする第１経路を設け、前記空気分離装置に寒冷としての液体酸素を供給する寒冷供給部を設けるとともに、前記寒冷供給部から前記熱交換器に液体酸素を供給可能とする第２経路を設け、前記第１経路と前記第２経路とを接続し、前記原料空気の一部を前記熱交換器に導き、冷却する第３経路を設け、前記熱交換器で冷却された前記原料空気の一部を、前記精留塔に導入する第４経路を設け、前記熱交換器において液体酸素の気化した酸素ガスを取り出す第５経路とを設けたことを特徴とする。
【０００８】
[作用]
本発明の空気液化分離装置は、原料空気の一部を前記主熱交換器を経由させずに冷却する熱交換器を設けるとともに、原料空気を前記熱交換器に導き、前記液体酸素と熱交換可能にする第３経路及び前記熱交換器で冷却された前記原料空気の一部を、前記精留塔に導入する第４経路を設けてあるから、原料空気の主な部分を主熱交換器を経由して冷却した後、精留塔に導くとともに、原料空気の一部を、前記主熱交換器とは別途、前記熱交換器において冷却し、前記精留塔に導くことができる。
ここで、前記主凝縮器部から液体酸素をパージ可能とする第１経路を設けるとともに、前記空気液化分離装置に寒冷としての液体酸素を供給する寒冷供給部を設け、前記寒冷供給部から前記熱交換器に液体酸素を供給可能とする第２経路を設けたから、前記主凝縮器部に可燃性物質が貯留されるのを防止することができるとともに、前記パージされる液体酸素及び寒冷供給部からの液体酸素によって前記原料空気の一部を冷却させることができる。そして、前記熱交換器において液体酸素の気化した酸素ガスを取り出す第５経路とを設けたことによって、前記両液体酸素が熱交換の際に気化した酸素ガスを取り出すことができる。
【０００９】
即ち、本発明の空気液化分離装置は、前記熱交換器にて、前記原料空気の一部は、前記精留塔の主凝縮器部及び前記寒冷供給部からの液体酸素により冷却され寒冷を得て高圧精留塔下部に供給され、一方、前記主凝縮器部及び前記寒冷供給部からの液体酸素は、前記原料空気の一部により強制的に気化され酸素ガスとして回収される。だから、寒冷供給部から液体酸素を主凝縮器部に供給する従来装置の如く、前記寒冷供給部から供給される液体酸素中の可燃性物質の含有量に注意を払うことなく、原料空気中の可燃性物質含有量のみに留意し、主凝縮器部からの液体酸素パージ量を決定し、前記主凝縮器部に貯留される可燃性物質の濃度を基準値以下に抑えることができる。
【００１０】
ここで、空気液化分離装置に必要な冷熱は、通常、寒冷を供給することでまかなわれるが、寒冷供給部からの液体酸素は、原料空気の一部と熱交換を行う熱交換器に導かれる一方、その熱交換器において熱交換された原料空気が精留塔に導かれるから、前記寒冷供給部からの液体酸素は前記精留塔へは直接導入されず、前記液体酸素の有する冷熱のみが前記原料空気の一部を介して前記精留塔へ導入されることになる。したがって、前記液体酸素は、たとえ可燃性物質を含有していたとしても、冷熱を前記精留塔へ供給する機能を果たしながら、可燃性物質を前記精留塔に導入することなく、酸素ガスとして取り出せることになる。なお、このようにして取り出された酸素ガスは、通常、製品として用いられる。また、前記主凝縮器部からパージされた液体酸素についても、前記熱交換器に導入されるとともに、冷熱を前記原料空気の一部に与えた後、酸素ガスとして取り出されるから、冷熱を廃棄せずに回収して、有効利用することができる。
【００１１】
したがって、寒冷供給部からの液体酸素を、原料空気の一部を冷却することに利用し、その冷却された原料空気により精留塔に対して供給されるべき寒冷をまかなうから、エネルギーの無駄がなく、かつ、前記精留塔内での可燃性物質の貯留も防げ、さらに、その可燃性物質をパージするのに取り出された液体酸素の冷熱も同時に有効利用することができるようになった。
【００１２】
また、前記第１経路と前記第２経路を設け、前記第１経路と前記第２経路とを接続してあるから、空気液化分離装置の運転起動時においては、前記寒冷供給部からの寒冷としての液体酸素を、前記第２経路を経由して前記第１経路から液体酸素を前記主凝縮器部に供給することで、直接的に前記精留塔に冷熱を供給できる。そのため、空気液化分離装置の起動を円滑に行わせることができ、迅速に定常的な運転が開始できるようになる。
また、定常運転時においては、前記寒冷供給部からの寒冷としての液体酸素を、前記寒冷供給部から前記第２経路を経由して前記熱交換器に導入すると同時に、前記主凝縮器部からの液体酸素を、前記第１経路を経由して、前記熱交換器にパージして、原料空気の一部を介して冷熱を精留塔に供給することができる。そのため、前記寒冷供給部の液体酸素中の不純物としての可燃性物質を主凝縮器部に導入することなく、精留塔への冷熱供給を円滑に行えるようになる。
【００１３】
【発明の効果】
その結果、低圧精留塔下部の主凝縮器部近傍に可燃性物質が蓄積するのを、より確実に抑えることができるようになった。
【００１４】
【発明の実施の形態】
本発明の空気液化分離装置を図面にしたがって説明する。
図１に示すように、本発明の空気液化分離装置は、外部から取り入れた原料空気を主熱交換器７で液化点付近まで冷却し、精留塔９に導入する経路を有し、外部から取り入れた原料空気の圧縮を行う圧縮機１、圧縮された原料空気を冷却する冷却器３、二酸化炭素及び水等の不純物の吸着除去を行う除炭乾燥器５を設けて、原料空気を順に導く構成としてある。その圧縮、冷却、除炭された原料空気を廃ガス等を利用して液化点付近まで冷却する主熱交換器７を設け、冷却された原料空気を導いて精留を行う精留塔９を設けてある。
前記精留塔９は、前記原料空気の予備精留を行う高圧精留塔１１及び空気の最終分離を行う低圧精留塔１２、高圧精留塔１１と低圧精留塔１２の間にあって低圧精留塔１２に対してはリボイラー、高圧精留塔１１に対してはコンデンサーの働きを行う主凝縮器部１９から構成される。
また、原料空気の一部を前記主熱交換器７を経由させずに冷却する熱交換器１６を設け、原料空気を前記熱交換器１６に導き、前記液体酸素と熱交換可能にする第３経路と前記主凝縮器部１９から液体酸素をパージ可能とする第１経路を設け、前記空気液化分離装置に寒冷としての液体酸素を供給する寒冷供給部１７を設けるとともに、前記寒冷供給部１７から前記熱交換器１６に液体酸素を供給可能とする第２経路を設け、さらに、前記熱交換器１６において液体酸素の気化した酸素ガスを取り出す第５経路とを設けてある。
【００１５】
上述の構成により、除塵用のフィルタを通じた原料空気は、前記圧縮機１に取り入れられ、圧縮機１により６．５ｋｇ／ｃｍ2Ｇのに圧縮された後、配管２を 通り冷却器（フレオン冷却器）３に導入され、この冷却器３で約５℃に予備冷却された後、配管４を通って切替式の除炭乾燥器５の一方の吸着塔５ａに導入され、この一方の吸着塔５ａにおいて、圧縮された原料空気中の二酸化炭素及び水等が除去され、配管６Ａを通り、配管６Ｂを介して、主熱交換器７に導入される。主熱交換器７に送られた原料空気は、主熱交換器７にて熱交換され、液化点近くまで冷却される。そして、冷却された原料空気は、配管８Ａを通り、配管８Ｂを介して、精留塔９の高圧精留塔１１に導入される。
このとき、前記吸着塔５ａの運転中には、前記除炭乾燥器の他方の吸着塔５ｂは、ヒータ２８で加熱された配管２７からの廃ガスによって再生されており、前記吸着塔５ａが吸着飽和したときには、交互に切り替えて運転できる構成にしてある。
【００１６】
高圧精留塔１１に導入された原料空気は、底部には酸素濃縮状態の液体空気を製出し、高圧精留塔１１の頂部に、窒素ガスを製出する。前記酸素富化液体空気は環流液として低圧精留塔に供給される。また、前記窒素ガスは、低圧精留塔１２の頂部へ供給する還流液として働くとともに、同時に低圧精留塔１２の底部に熱源を与える。高圧精留塔１１頂部では窒素ガスの一部が液化され還流液として下部精留部１３を流下し、上昇してくる空気と気液接触して精留する。一方、窒素ガスの残部は、高圧精留塔１１上部から、膨張弁Ｖ1で約１．１ｋｇ／ｃｍ2Ｇに膨張された後、低圧精留塔１２の上部精留部の上部に導かれる。
高圧精留塔１１の底部から配管１８を通して導出された酸素濃縮液体は、膨張弁Ｖ2で約１．２ｋｇ／ｃｍ2Ｇに膨張された後、低圧精留塔１２の第一上部精留部１４Ａの下部２３に導かれる。低圧精留塔１２は、空気の最終分離を行うもので、塔底に酸素を、頂部に窒素を製出する。低圧精留塔１２は、その中間にある空間２３から上は窒素の回収塔として、また、下部は酸素の濃縮塔として働く。低圧精留塔１２の頂部の廃ガスは、配管２４を通して主熱交換器７に導入され、低圧精留塔１２の底部の主凝縮器部１９の下に位置する主凝縮器部１９に貯留された液化酸素のうち高圧精留塔１１の窒素ガスにより気化された酸素ガスは、配管２５を通って主熱交換器７に導入される。前記酸素ガスは、主熱交換器７で圧縮原料空気と熱交換され、配管２６Ａ及び配管２６Ｂ（製品酸素ガス回収路）を通り、約１ｋｇ／ｃｍ2Ｇの圧力で常温の製品酸素ガス（ＧＯ２）として得られ る。また、前記廃ガスは、配管２７を通り、前記主熱交換器７で熱交換した後、約１．０ｋｇ／ｃｍ2Ｇの圧力で常温となって切替式除炭乾燥器５の再生すべき 吸着塔５ｂに送られ、前記吸着塔５ｂの再生ガスとして用いられる。また、前記主凝縮器部１９に貯留される液体酸素は、前記第１経路からパージされる。
【００１７】
また、同時に窒素ガスが必要な場合には、窒素ガスは、高圧精留塔１１の下部精留部１３の上部から配管２９を通して約６ｋｇ／ｃｍ2Ｇの圧力で取り出され 、主熱交換器７で原料空気との熱交換に供された後、常温の製品窒素ガス（ＧＮ２）として配管３０を通って外部に導出される。
【００１８】
前記主凝縮器部１９からパージされた前記液体酸素は、前記第１経路を経由して前記熱交換器１６に導入され、前記第３経路から導入される原料空気と熱交換した後、前記第５経路を経由して前記配管２６Ｂを通じて回収される。一方、前記熱交換器１６で冷熱を回収した前記原料空気は、前記第４経路を経由して前記精留塔に導入される。
また、前記第１経路と前記第２経路は接続されており、配管１５Ｄには開閉自在な弁Ｖ4が設けられている。このように、前記主凝縮器部から前記液体酸素をパージ可能、かつ、前記主凝縮器部に液体酸素を供給可能とする第１経路と寒冷供給用液体酸素を供給可能とする第２経路が連結しているので、装置の起動時等大量の寒冷供給用液体酸素が精留塔に必要な場合にも、前記弁Ｖ4の開閉を調節することで容易に対応できる。
【００１９】
即ち、空気液化分離装置の運転起動時においては、配管１５Ｄに設けられた前記弁Ｖ4を閉じることで、前記寒冷供給部からの寒冷としての液体酸素を、前記 寒冷供給部から主凝縮器部に導入することで、直接的に前記精留塔に冷熱を供給できる。そのため、空気液化分離装置の起動を円滑に行わせることができ、迅速に定常的な運転が開始できるようになる。また、定常運転時においては、配管１５Ｄに設けられた前記弁Ｖ4を開くことで、前記寒冷供給部からの寒冷としての 液体酸素を、前記寒冷供給部から前記熱交換器に導入して、原料空気の一部を介して冷熱を精留塔に供給することができる。そのため、前記寒冷供給部の液体酸素中の不純物としての可燃性物質を主凝縮器部に導入することなく、精留塔への冷熱供給を円滑に行えるようになる。
【００２０】
即ち、通常運転時には、前記主凝縮器部１９からは酸素に富む液体が配管１５Ａにより取り出される。この液体には原料空気中の炭化水素類二酸化炭素等が濃縮されているので、この液体を連続的に取り出すことで、精留塔９内での炭化水素類の蓄積は防止される。配管１５Ａの炭化水素類の濃縮された液体は、配管１５Ｃを通って、熱交換器１６に送られる。この空気液化分離装置５０に必要な冷熱の一部は、液化酸素貯槽１７内に貯留された液化酸素により賄われ、この液化酸素は、配管１５Ｂを通して取り出され、減圧弁Ｖ3により約１．２ｋｇ／ｃｍ2Ｇの圧力に減圧された後、配管１５Ｃを通って熱交換器１６に送られる。この熱交換器１６には、配管６Ａから配管６Ｃを通って常温の原料空気の一部が導かれ、前記配管１５Ｃからの液体はこの常温の空気と間接熱交換することにより強制的に気化され、配管１５Ｄを通って、配管２６Ｂを通り、常温の製品酸素ガス （ＧＯ２）として得られる。熱交換器１６において液体酸素の加熱気化に用いられた一部の空気は自らは冷却されて配管６Ｄから取り出され、配管８Ｂを通り、高圧精留塔１１の空間１０に導入される。
【００２１】
一方、装置立ち上げ時には、前記液体酸素槽１７からの液体酸素は、配管１５Ｂを通して取り出され、配管１５Ａを経由し、前記液体酸素貯留槽に貯留される。これにより、主凝縮器部１９で必要な寒冷としての液体酸素を、前記液体酸素貯留槽１７から直接的に前記主凝縮器部１９に導入することができ、装置立ち上げ時には迅速かつ的確な液体酸素の供給を行うことができるのである。
【００２２】
沸点の異なる成分から混合液体を気化させる場合、徐々に気化させると一部成分のみが気化して他成分が液体中に残り濃縮される。従って、それを防止するために、配管１５Ｃにおける液体酸素の量に比較して、配管６Ａにおける常温空気は相当量使用し、強制的に液化酸素の気化を行う。
【図面の簡単な説明】
【図１】本願発明空気液化分離装置のフローを示す図
【図２】従来の空気液化分離装置のフローを示す図
【符号の説明】
１ 圧縮機
３ 冷却器
５ 除炭乾燥器
７ 主熱交換器
９ 精留塔
１１ 高圧精留塔
１２ 低圧精留塔
１６ 熱交換器
１７ 寒冷供給部
１９ 主凝縮器部
５０ 空気液化分離装置[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an air liquefaction separation apparatus for producing oxygen gas by liquefying and rectifying air.
[0002]
[Prior art]
Conventionally, as this type of air liquefaction separation apparatus, as shown in FIG. 2, a compressor 1 that compresses raw material air taken from the outside, a cooler 3 that cools the compressed raw material air, carbon dioxide, water, and the like Is provided with a decarburization dryer 5 for adsorbing and removing impurities, and the raw material air is sequentially guided, and the compressed, cooled, and decarburized raw material air is liquefied in the main heat exchanger 7 using waste gas or the like. It is known that a rectifying column is provided which cools to a point and guides the cooled raw air to perform rectification. In such a case, the rectification column includes a high-pressure rectification column 11 that performs preliminary rectification of the raw material air, a low-pressure rectification column 12 that performs final separation of air, a high-pressure rectification column 11 and a low-pressure rectification column 12. A reboiler is used for the low-pressure rectification column 12 and a main condenser unit 19 is used for the high-pressure rectification column 11. Further, the cooling for the rectification tower is configured to provide a cooling supply unit 17 to supply liquid oxygen to the main condenser unit 19.
[0003]
In such an air liquefaction separation apparatus, normally, liquid oxygen is directly introduced from the cold supply unit 17 into the main condenser unit 19 and used as cold. The supplied liquid oxygen exchanges heat with the main condenser section 19 and is used as a raw material for product oxygen.
Here, although a small amount of flammable substances such as hydrocarbons contained in the raw air are removed to some extent by the decarburization dryer 5, those that could not be removed are introduced into the rectifying column 9. End up. Then, from the relationship with the vapor pressure equilibrium and the like, combustible substances such as hydrocarbons are gradually concentrated together with liquid oxygen in the lower part of the low-pressure rectification column. Such a configuration is often used for a small air liquefaction separation device from the viewpoint of cost, etc., but in order to avoid explosion of the combustible substance in the concentrated liquid oxygen, the combustible substance is concentrated. The security management of the main condenser section 19 is extremely important. Therefore, it is necessary to take a procedure for purging a small amount of liquid oxygen from the main condenser section 19 so that the amount of combustible substance in the main condenser section 19 is always below a predetermined value. Was discarded after being purged.
[0004]
Further, when the purged gas is discarded as it is, the cold heat is also discarded, which is uneconomical. Therefore, a heat exchanger is provided in the air liquefaction separation device, and a path for leading the liquid oxygen purged from the main condenser section 19 in the rectifying column 9 to the heat exchanger 16 is vaporized by the heat exchanger 16. A path for taking out the oxygen gas, a path for guiding the raw air to the heat exchanger 16 and enabling heat exchange, and a path for guiding the raw air cooled in the heat exchanger 16 to the rectification column 9 are provided, There has been proposed an air liquefaction separation apparatus capable of recovering the cold heat of liquid oxygen purged from the main condenser section 19.
[0005]
[Problems to be solved by the invention]
However, even in such an air liquefaction / separation apparatus, liquid oxygen supplied as cold from the cold supply unit 17 is directly introduced into the main condenser unit 19 from the cold supply unit 17. Therefore, even if liquid oxygen is purged in order to prevent an increase in the amount of combustible substances in the main condenser section 19, a cold supply section 17 that supplies cold to the air liquefaction separation device is supplied to the main condenser section 19. Liquid oxygen is supplied as cold. Since the liquid oxygen in the cold supply unit 17 contains a small amount of combustible material as an impurity, in order to prevent an increase in the amount of combustible material in the main condenser unit 19, the main condensation is performed. It is necessary to pay attention not only to the liquid oxygen purged from the vessel part 19 but also to the combustible substance in the liquid oxygen as the cold from the cold supply part 17. That is, in order to prevent an increase in the amount of combustible material in the main condenser unit 19, the low-pressure rectification is performed in consideration of both combustible materials in liquid oxygen as cold from the cold supply unit 17. Liquid oxygen had to be purged from the lower part of the column 12, and there was room for improvement.
[0006]
Therefore, an object of the present invention is to liquefy air that can suppress the accumulation of combustible substances in the main condenser section 19 without being affected by the content of combustible substances in the liquid oxygen from the cold supply section 17. It is to provide a separation device. That is, to provide an air liquefaction separation apparatus capable of setting the purge amount of liquid oxygen from the main condenser unit 19 without being affected by the combustible substance content in the liquid oxygen from the cold supply unit 17. is there.
[0007]
[Means for Solving the Problems]
The structure of the air liquefaction separation apparatus of the present invention for achieving the above object is the air liquefaction separation apparatus having a path for cooling the raw material air taken from the outside to the vicinity of the liquefaction point by the main heat exchanger and introducing it to the rectification column. A heat exchanger that cools a part of the raw air without going through the main heat exchanger, can be purged of liquid oxygen from the main condenser section in the rectification tower, and the main condenser section A first path that can supply liquid oxygen is provided, a cold supply unit that supplies liquid oxygen as cold is provided in the air separation device, and liquid oxygen can be supplied from the cold supply unit to the heat exchanger. A second path is provided, the first path and the second path are connected, a part of the raw material air is guided to the heat exchanger, and a third path for cooling is provided and cooled by the heat exchanger. Part of the raw air is introduced into the rectification column The fourth path provided, characterized by providing a fifth path to take out the vaporized oxygen gas in the liquid oxygen in the heat exchanger.
[0008]
[Action]
The air liquefaction separation apparatus of the present invention is provided with a heat exchanger that cools part of the raw material air without passing through the main heat exchanger, and guides the raw material air to the heat exchanger to exchange heat with the liquid oxygen. Since the third path for enabling and the fourth path for introducing a part of the raw air cooled by the heat exchanger into the rectification column are provided, the main part of the raw air is used as the main heat exchanger. After cooling through the refrigeration tower, it is led to the rectification tower, and part of the raw material air can be cooled in the heat exchanger separately from the main heat exchanger and led to the rectification tower.
Here, a first path that allows purging of liquid oxygen from the main condenser section is provided, a cold supply section that supplies liquid oxygen as cold to the air liquefaction separation device is provided, and the heat supply from the cold supply section Since the second path enabling liquid oxygen to be supplied to the exchanger is provided, it is possible to prevent the combustible material from being stored in the main condenser section, and from the purged liquid oxygen and cold supply section. A part of the raw material air can be cooled by the liquid oxygen. Then, by providing a fifth path for taking out the oxygen gas in which the liquid oxygen is vaporized in the heat exchanger, it is possible to take out the oxygen gas in which the two liquid oxygens are vaporized during the heat exchange.
[0009]
That is, in the air liquefaction separation apparatus of the present invention, in the heat exchanger, a part of the raw material air is cooled by liquid oxygen from the main condenser part and the cold supply part of the rectification tower to obtain cold. On the other hand, liquid oxygen from the main condenser section and the cold supply section is forcibly vaporized by a part of the raw air and recovered as oxygen gas. Therefore, as in the conventional apparatus for supplying liquid oxygen from the cold supply unit to the main condenser unit, the content of the combustible substance in the liquid oxygen supplied from the cold supply unit is not paid attention to in the raw material air. By paying attention only to the combustible substance content, the amount of liquid oxygen purge from the main condenser section can be determined, and the concentration of the combustible substance stored in the main condenser section can be suppressed to a reference value or less.
[0010]
Here, the cold heat necessary for the air liquefaction separation apparatus is usually supplied by supplying cold, but the liquid oxygen from the cold supply unit is led to a heat exchanger that exchanges heat with a part of the raw material air. On the other hand, since the raw material air heat-exchanged in the heat exchanger is guided to the rectification tower, the liquid oxygen from the cold supply section is not directly introduced into the rectification tower, and only the cold heat of the liquid oxygen is contained. It will be introduced into the rectification tower through a part of the raw air. Therefore, even if the liquid oxygen contains a flammable substance, it does not introduce a flammable substance into the rectifying tower while serving as a function of supplying cold heat to the rectifying tower. You can take it out. The oxygen gas extracted in this way is usually used as a product. Also, liquid oxygen purged from the main condenser section is introduced into the heat exchanger, and after cooling is given to a part of the raw air, it is taken out as oxygen gas, so that the cooling heat can be discarded. It can be collected and used effectively.
[0011]
Therefore, the liquid oxygen from the cold supply unit is used to cool a part of the raw material air, and the cooled raw material air covers the cold to be supplied to the rectification tower, so that energy is wasted. In addition, storage of combustible substances in the rectification column can be prevented, and the cold heat of liquid oxygen taken out for purging the combustible substances can be used effectively at the same time.
[0012]
In addition, since the first path and the second path are provided and the first path and the second path are connected, when the operation of the air liquefaction separation apparatus is started, the cold supply from the cold supply unit By supplying liquid oxygen from the first path to the main condenser section via the second path, cold heat can be directly supplied to the rectification tower. Therefore, the air liquefaction separation device can be started up smoothly, and a steady operation can be started quickly.
Further, during steady operation, liquid oxygen as cold from the cold supply unit is introduced into the heat exchanger from the cold supply unit via the second path, and at the same time from the main condenser unit. Liquid oxygen can be purged to the heat exchanger via the first path, and cold heat can be supplied to the rectification tower via part of the feed air. For this reason, it is possible to smoothly supply cold heat to the rectifying column without introducing a flammable substance as an impurity in the liquid oxygen of the cold supply section into the main condenser section .
[0013]
【The invention's effect】
As a result, accumulation of combustible substances in the vicinity of the main condenser part at the lower part of the low-pressure rectification column can be more reliably suppressed.
[0014]
DETAILED DESCRIPTION OF THE INVENTION
The air liquefaction separation apparatus of this invention is demonstrated according to drawing.
As shown in FIG. 1, the air liquefaction separation apparatus of the present invention has a path for cooling the raw material air taken from the outside to the vicinity of the liquefaction point by the main heat exchanger 7 and introducing it to the rectification tower 9, from the outside. A compressor 1 that compresses the introduced raw material air, a cooler 3 that cools the compressed raw material air, and a decarburizer dryer 5 that adsorbs and removes impurities such as carbon dioxide and water are provided to sequentially guide the raw material air. As a configuration. A main heat exchanger 7 that cools the compressed, cooled, and decarburized raw material air to the vicinity of the liquefaction point using waste gas or the like is provided, and a rectifying column 9 that conducts rectification by introducing the cooled raw material air It is provided.
The rectification column 9 includes a high-pressure rectification column 11 that performs preliminary rectification of the raw material air, a low-pressure rectification column 12 that performs final separation of air, and a low-pressure rectification column 12 between the high-pressure rectification column 11 and the low-pressure rectification column 12. A reboiler is used for the distillation column 12 and a main condenser section 19 that functions as a condenser for the high-pressure rectification column 11.
Also, a heat exchanger 16 that cools a part of the raw material air without passing through the main heat exchanger 7 is provided, and the raw material air is guided to the heat exchanger 16 to allow heat exchange with the liquid oxygen. A path and a first path that allows purging of liquid oxygen from the main condenser section 19 are provided, a cold supply section 17 that supplies liquid oxygen as cold to the air liquefaction separation device is provided, and from the cold supply section 17 A second path through which liquid oxygen can be supplied to the heat exchanger 16 is provided, and a fifth path through which oxygen gas vaporized from the liquid oxygen is taken out in the heat exchanger 16 is provided.
[0015]
With the above-described configuration, the raw material air that has passed through the dust removal filter is taken into the compressor 1 and compressed to 6.5 kg / cm 2 G by the compressor 1, and then passed through the pipe 2 to cool a cooler (Freon cooling). 3), precooled to about 5 ° C. by the cooler 3, and then introduced into one adsorption tower 5a of the switch-type decarburization dryer 5 through the pipe 4, and this one adsorption tower In 5a, carbon dioxide, water, and the like in the compressed raw material air are removed and introduced into the main heat exchanger 7 through the pipe 6A and the pipe 6B. The raw material air sent to the main heat exchanger 7 is heat-exchanged in the main heat exchanger 7 and cooled to near the liquefaction point. And the cooled raw material air is introduce | transduced into the high pressure rectification column 11 of the rectification column 9 through the piping 8A through the piping 8A.
At this time, during the operation of the adsorption tower 5a, the other adsorption tower 5b of the decarburization dryer is regenerated by the waste gas from the pipe 27 heated by the heater 28, and the adsorption tower 5a is adsorbed. When saturated, it can be operated by switching alternately.
[0016]
The raw material air introduced into the high-pressure rectification column 11 produces oxygen-enriched liquid air at the bottom and produces nitrogen gas at the top of the high-pressure rectification column 11. The oxygen-enriched liquid air is supplied as a reflux liquid to the low-pressure rectification column. The nitrogen gas serves as a reflux liquid to be supplied to the top of the low pressure rectification column 12 and simultaneously provides a heat source to the bottom of the low pressure rectification column 12. A part of the nitrogen gas is liquefied at the top of the high-pressure rectification column 11 and flows down as a reflux liquid through the lower rectification unit 13 and undergoes rectification by contacting the rising air with gas and liquid. On the other hand, the remainder of the nitrogen gas is expanded from the upper part of the high pressure rectification column 11 to about 1.1 kg / cm 2 G by the expansion valve V 1 and then led to the upper part of the upper rectification unit of the low pressure rectification column 12. .
The oxygen concentrated liquid led out from the bottom of the high pressure rectification column 11 through the pipe 18 is expanded to about 1.2 kg / cm 2 G by the expansion valve V 2 , and then the first upper rectification unit of the low pressure rectification column 12. It is led to the lower part 23 of 14A. The low-pressure rectification column 12 performs final separation of air, and produces oxygen at the bottom and nitrogen at the top. The low-pressure rectification column 12 functions as a nitrogen recovery column from the space 23 in the middle, and the lower portion functions as an oxygen concentration column. The waste gas at the top of the low-pressure rectification column 12 is introduced into the main heat exchanger 7 through the pipe 24 and is stored in the main condenser unit 19 located below the main condenser unit 19 at the bottom of the low-pressure rectification column 12. Of the liquefied oxygen, oxygen gas evaporated by the nitrogen gas in the high pressure rectification column 11 is introduced into the main heat exchanger 7 through the pipe 25. The oxygen gas is heat-exchanged with the compressed raw material air in the main heat exchanger 7, passes through the pipe 26A and the pipe 26B (product oxygen gas recovery path), and is a product oxygen gas (GO2) at room temperature at a pressure of about 1 kg / cm 2 G. ). The waste gas passes through the pipe 27 and is heat-exchanged by the main heat exchanger 7, and then becomes room temperature at a pressure of about 1.0 kg / cm 2 G. The switch-type decarburization dryer 5 should be regenerated. It is sent to the adsorption tower 5b and used as a regeneration gas for the adsorption tower 5b. The liquid oxygen stored in the main condenser unit 19 is purged from the first path.
[0017]
When nitrogen gas is required at the same time, the nitrogen gas is taken out from the upper part of the lower rectifying section 13 of the high-pressure rectifying column 11 through the pipe 29 at a pressure of about 6 kg / cm 2 G, and the main heat exchanger 7 Then, after being subjected to heat exchange with the raw material air, it is led out through the piping 30 as product nitrogen gas (GN2) at normal temperature.
[0018]
The liquid oxygen is purged from the main condenser 19, the first path via the introduced into the heat exchanger 16, after feed air exchanges heat introduced from the third path, the first It is collected through the pipe 26B via five paths . On the other hand, the raw material air recovered from the cold heat by the heat exchanger 16 is introduced into the rectification tower via the fourth path.
Further, the first path and the second path are connected, and a valve V4 that can be freely opened and closed is provided in the pipe 15D. As described above, the first path that allows the liquid oxygen to be purged from the main condenser section and the liquid oxygen to be supplied to the main condenser section and the second path that can supply the liquid oxygen for cold supply are provided. Since they are connected, even when a large amount of cold supply liquid oxygen is required for the rectification column, such as when the apparatus is started up, it can be easily handled by adjusting the opening and closing of the valve V4.
[0019]
That is, at the start of the operation of the air liquefaction separation apparatus, by closing the valve V 4 provided in the pipe 15D, liquid oxygen as cold from the cold supply unit is supplied from the cold supply unit to the main condenser unit. By introducing into the rectifier, cold heat can be directly supplied to the rectification column. Therefore, the air liquefaction separation device can be started up smoothly, and a steady operation can be started quickly. In the steady operation, by opening the valve V 4 which is provided in the pipe 15D, the liquid oxygen as cold from the cold feed section, is introduced into the heat exchanger from the cold feed section, Cold heat can be supplied to the rectification tower via part of the raw air. For this reason, it is possible to smoothly supply cold heat to the rectifying column without introducing a flammable substance as an impurity in the liquid oxygen of the cold supply section into the main condenser section.
[0020]
That is, during normal operation, a liquid rich in oxygen is taken out from the main condenser section 19 through the pipe 15A. Since this liquid is concentrated with hydrocarbons such as carbon dioxide in the raw air, accumulation of hydrocarbons in the rectifying column 9 is prevented by continuously removing this liquid. The hydrocarbon-enriched liquid in the pipe 15A is sent to the heat exchanger 16 through the pipe 15C. Some of the cold required for the air separation plant 50 is covered by the pooled liquid oxygen into the liquid oxygen storage tank 17, the liquid oxygen is withdrawn through a pipe 15B, about 1.2kg the pressure reducing valve V 3 After being depressurized to a pressure of / cm 2 G, it is sent to the heat exchanger 16 through the pipe 15C. A part of room temperature raw air is led from the pipe 6A through the pipe 6C to the heat exchanger 16, and the liquid from the pipe 15C is forcibly vaporized by indirect heat exchange with the room temperature air. Through the pipe 15D, and through the pipe 26B, it is obtained as room temperature product oxygen gas (GO2). A part of the air used for heating and vaporizing the liquid oxygen in the heat exchanger 16 is cooled by itself, taken out from the pipe 6D, and introduced into the space 10 of the high-pressure rectification column 11 through the pipe 8B.
[0021]
On the other hand, when the apparatus is started up, liquid oxygen from the liquid oxygen tank 17 is taken out through the pipe 15B and stored in the liquid oxygen storage tank via the pipe 15A. Thereby, the liquid oxygen as the cold required in the main condenser unit 19 can be directly introduced into the main condenser unit 19 from the liquid oxygen storage tank 17, and the liquid can be quickly and accurately set up when the apparatus is started up. Oxygen can be supplied.
[0022]
When the mixed liquid is vaporized from components having different boiling points, when it is gradually vaporized, only some components are vaporized and other components remain in the liquid and are concentrated. Therefore, in order to prevent this, a considerable amount of room temperature air in the pipe 6A is used as compared with the amount of liquid oxygen in the pipe 15C to forcibly vaporize liquefied oxygen.
[Brief description of the drawings]
FIG. 1 is a diagram showing a flow of an air liquefaction separation apparatus of the present invention. FIG. 2 is a diagram showing a flow of a conventional air liquefaction separation apparatus.
DESCRIPTION OF SYMBOLS 1 Compressor 3 Cooler 5 Decarburization dryer 7 Main heat exchanger 9 Rectifying tower 11 High pressure rectifying tower 12 Low pressure rectifying tower 16 Heat exchanger 17 Cold supply part 19 Main condenser part 50 Air liquefaction separation apparatus

Claims (1)

外部から取り入れた原料空気を主熱交換器で液化点付近まで冷却し、精留塔に導入する経路を有する空気液化分離装置において、
原料空気の一部を前記主熱交換器を経由せずに冷却する熱交換器を設け、
前記精留塔内の主凝縮器部から液体酸素をパージ可能、かつ、前記主凝縮器部に液体酸素を供給可能とする第１経路を設け、
前記空気分離装置に寒冷としての液体酸素を供給する寒冷供給部を設けるとともに、前記寒冷供給部から前記熱交換器に液体酸素を供給可能とする第２経路を設け、
前記第１経路と前記第２経路とを接続し、
前記原料空気の一部を前記熱交換器に導き、冷却する第３経路を設け、
前記熱交換器で冷却された前記原料空気の一部を、前記精留塔に導入する第４経路を設け、
前記熱交換器において液体酸素の気化した酸素ガスを取り出す第５経路とを設けたことを特徴とする空気液化分離装置。In the air liquefaction separation apparatus having a path for cooling the raw material air taken from the outside to the vicinity of the liquefaction point in the main heat exchanger,
A heat exchanger that cools part of the raw air without going through the main heat exchanger is provided,
Providing a first path capable of purging liquid oxygen from the main condenser section in the rectification column and supplying liquid oxygen to the main condenser section ;
A cold supply unit that supplies liquid oxygen as cold to the air separation device is provided, and a second path that allows liquid oxygen to be supplied from the cold supply unit to the heat exchanger is provided,
Connecting the first path and the second path;
Providing a third path for guiding a part of the raw material air to the heat exchanger for cooling;
Providing a fourth path for introducing a part of the raw material air cooled by the heat exchanger into the rectification tower;
An air liquefaction separation apparatus comprising a fifth path for taking out oxygen gas in which liquid oxygen is vaporized in the heat exchanger.
JP36705798A 1998-12-24 1998-12-24 Air liquefaction separator Expired - Fee Related JP3969874B2 (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104067079A (en) * 2011-03-18 2014-09-24 乔治洛德方法研究和开发液化空气有限公司 Apparatus and method for separating air by cryogenic distillation

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5278356B2 (en) * 2010-03-08 2013-09-04 Ｊｆｅスチール株式会社 Cold separation method for air separation device

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104067079A (en) * 2011-03-18 2014-09-24 乔治洛德方法研究和开发液化空气有限公司 Apparatus and method for separating air by cryogenic distillation

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