JP2006329615A - Method and device for separating air by low temperature distillation - Google Patents

Method and device for separating air by low temperature distillation Download PDF

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JP2006329615A
JP2006329615A JP2006139954A JP2006139954A JP2006329615A JP 2006329615 A JP2006329615 A JP 2006329615A JP 2006139954 A JP2006139954 A JP 2006139954A JP 2006139954 A JP2006139954 A JP 2006139954A JP 2006329615 A JP2006329615 A JP 2006329615A
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air
turbine
pressure
column
heat exchanger
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Gabbita Venkata Maruthi Shyamala Prasad
ガッビタ・ベンカタ・マルスィ・シャマラ・プラサド
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/04151—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
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04151—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
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/0429—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
    • 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
    • F25J3/0429—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—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
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2

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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)

Abstract

<P>PROBLEM TO BE SOLVED: To provide an improved method for separating air by low temperature distillation. <P>SOLUTION: The air is compressed to the first pressure in a compressor, cooled and refined, the air under the first pressure is compressed to the second pressure in the first and second booster compressors 11, 8, to be cooled thereafter in a heat exchanger 5, at least one part of the air under the second pressure fed to the heat exchanger is cooled to be liquefied and is fed to at least one column of a double column, at least one part of the air is compressed to intermediate pressure between the first pressure and the second pressure, in the first booster compressor, followed to be cooled, and is expanded in the first turbine 12 having the first inlet temperature, the first portion of the air expanded in the the first turbine is fed to a high-pressure column, the second portion of the air expanded in the the first turbine is fed to the heat exchanger to be heated, and the second portion of the heated air is expanded in the second turbine 9 and is returned to the heat exchanger to be heated further. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

本発明は、低温蒸留（cryogenic distillation）により空気を分離するための方法および装置に関する。本発明は、空気中に存在するガスの分離および液化に、および空気の蒸留のための装置に適用される。本発明は、２つンタービン中での空気の膨張による低温生産を用いた方法に関する。空気の一部は、冷（cold）タービンと呼ばれる第１のタービン中で膨張され、ついで、この第１のタービンからの流体が、温（warm）タービンと呼ばれる第２のタービン中で膨張される。   The present invention relates to a method and apparatus for separating air by cryogenic distillation. The invention applies to the separation and liquefaction of gases present in air and to equipment for the distillation of air. The present invention relates to a method using cold production by expansion of air in a two-turbine turbine. A portion of the air is expanded in a first turbine called a cold turbine, and then the fluid from this first turbine is expanded in a second turbine called a warm turbine. .

特許文献１において、全ての圧縮空気は、直列接続された２つのブースタ中で昇圧される。ついで、この空気は、冷却され、高圧タービン中で膨張され、その後、この空気の一部は低圧タービン中で再び膨張される。   In Patent Document 1, all compressed air is pressurized in two boosters connected in series. The air is then cooled and expanded in the high pressure turbine, after which a portion of the air is expanded again in the low pressure turbine.

この構成は、機械の非入手性により、大規模空気分離プラントにおける液体対ガス比を制限する。温ブースタおよび温膨張機を通る流れに大きな相違が存在する。
ＵＳ−Ａ−５１５７９２６ This configuration limits the liquid to gas ratio in large air separation plants due to machine unavailability. There are significant differences in the flow through the warm booster and the expander.
US-A-5157926

本発明は、低温蒸留により空気を分離するための改善された方法および装置を提供することを目的とする。   The present invention seeks to provide an improved method and apparatus for separating air by cryogenic distillation.

本発明によれば、高圧カラムと低圧カラムを備える二重カラムを少なくとも備える低温蒸留装置を用いる低温蒸留により空気を分離するための方法であって、空気を圧縮機中で第１の圧力に圧縮し、冷却し、および精製し、前記第１の圧力にある空気を第１および第２のブースタ圧縮機中で第２の圧力に圧縮した後、熱交換器中で冷却し、前記熱交換器に送られた前記第２の圧力にある空気の少なくとも一部を冷却し、液化し、および前記二重カラムの少なくとも１つのカラムに送り、該空気の少なくとも一部を、前記第１のブースタ圧縮機中で、前記第１の圧力と第２の圧力の中間の圧力に圧縮し、冷却し、および第１の入口温度を有する第１のタービン中で膨張させ、前記第１のタービン中で膨張された空気の第１の部分を前記高圧カラムに送り、前記第１のタービン中で膨張された空気の第２の部分を加温すべく前記熱交換器に送り、この加温された空気の第２の部分を、第２のタービン中で膨張させ、前記熱交換器に戻し、さらに加温する該方法が提供される。   According to the present invention, a method for separating air by cryogenic distillation using a cryogenic distillation apparatus comprising at least a double column comprising a high pressure column and a low pressure column, wherein the air is compressed to a first pressure in a compressor. Cooling, purifying, and compressing air at the first pressure to a second pressure in the first and second booster compressors and then cooling in a heat exchanger, the heat exchanger At least a portion of the air at the second pressure sent to is cooled, liquefied, and sent to at least one column of the dual column, wherein at least a portion of the air is compressed into the first booster In the machine, compressed to an intermediate pressure between the first pressure and the second pressure, cooled and expanded in a first turbine having a first inlet temperature and expanded in the first turbine A first portion of the conditioned air in the high pressure column To the heat exchanger to warm a second portion of the air expanded in the first turbine, and to pass the second portion of the warmed air in the second turbine The method is provided for expanding, returning to the heat exchanger and further warming.

本発明は、以下の特徴の１つまたはそれ以上を有し得る：
− 前記中間の圧力に圧縮された後、冷却された全ての空気を前記第１のタービンに送ること；
− 少なくとも１種の液体生成物が製造されること；
− 前記第１のブースタ圧縮機が、前記第１のタービンに連結され、前記第２のブースタ圧縮機が、前記第２のタービンに連結されること。 The present invention may have one or more of the following features:
-Sending all cooled air to the first turbine after being compressed to the intermediate pressure;
-At least one liquid product is produced;
The first booster compressor is connected to the first turbine and the second booster compressor is connected to the second turbine;

本発明のさらなる側面によると、高圧カラムと低圧カラムを備える二重カラム、圧縮機、第１および第２のタービン、第１および第２のブースタ圧縮機、熱交換器、第１の圧力にある空気を、前記圧縮機から、直列に接続された前記第１および第２のブースタ圧縮機に送るための手段、第２の圧力にある空気を、前記第２のブースタ圧縮機の出口から、前記熱交換器に送り、ついで前記二重カラムの少なくとも１つのカラムに送るための手段、前記第１のブースタ圧縮機から空気を取り出すための手段、前記第１のブースタ圧縮機から取り出された空気を前記熱交換器に送り、ついで前記第１のタービンに送るための手段、前記第１のタービンから空気を前記高圧カラムに送るための手段、前記第１のタービンから空気を熱交換器の冷末端（cold end）に送るための手段、前記第１のタービンから前記熱交換器に送られた空気を前記熱交換器の中間点から取り出すための手段、該取り出された空気を第２のタービンに送るための手段、並びに前記第２のタービンから空気を前記熱交換器へ戻すための手段を備える、低温蒸留により空気を分離するための装置が提供される。   According to a further aspect of the invention, a double column comprising a high pressure column and a low pressure column, a compressor, a first and a second turbine, a first and a second booster compressor, a heat exchanger, a first pressure Means for sending air from the compressor to the first and second booster compressors connected in series; air at a second pressure from the outlet of the second booster compressor; Means for sending to a heat exchanger and then to at least one column of the double column, means for taking air from the first booster compressor, air taken from the first booster compressor Means for sending to the heat exchanger and then to the first turbine, means for sending air from the first turbine to the high pressure column, air from the first turbine to the cold end of the heat exchanger (C old end), means for extracting air sent from the first turbine to the heat exchanger from an intermediate point of the heat exchanger, and sending the extracted air to the second turbine There is provided an apparatus for separating air by cryogenic distillation, comprising means for, and means for returning air from the second turbine to the heat exchanger.

本装置は、前記第１のブースタ圧縮機で圧縮された全ての空気を前記第１のタービンに送るための手段を有し得る。   The apparatus may have means for sending all the air compressed by the first booster compressor to the first turbine.

前記第１のブースタ圧縮機は、前記第１のタービンに連結され得、前記第２のブースタ圧縮機は、前記第２のタービンに連結され得る。   The first booster compressor may be coupled to the first turbine, and the second booster compressor may be coupled to the second turbine.

本装置は、アルゴンカラム、およびアルゴン富化流を前記低圧カラムからこのアルゴンカラムに送るための手段を有し得る。   The apparatus may have an argon column and means for sending an argon enriched stream from the low pressure column to the argon column.

以下、図面を参照しながら、本発明を説明する。
図１に示される空気蒸留装置は、ガス状および液状で酸素、窒素およびアルゴンを製造するためのものである。この装置は、二重蒸留カラム１を備え、これは、約６バール（絶対）で操作される高圧カラム２と、その上に設けられた、大気圧よりもやや高い圧力で操作される低圧カラム３を含む。カラム２のヘッド部分内のガス（窒素）は、蒸発器−凝縮器４により、カラム３のバット（vat）部分内の液体（酸素）と間接的熱交換関係にある。 Hereinafter, the present invention will be described with reference to the drawings.
The air distillation apparatus shown in FIG. 1 is for producing oxygen, nitrogen and argon in gaseous and liquid form. This apparatus comprises a double distillation column 1, which comprises a high pressure column 2 operated at about 6 bar (absolute) and a low pressure column provided thereon and operated at a pressure slightly higher than atmospheric pressure. 3 is included. The gas (nitrogen) in the head portion of the column 2 is in an indirect heat exchange relationship with the liquid (oxygen) in the vat portion of the column 3 by the evaporator-condenser 4.

この装置は、また、熱交換関係にある流体の向流循環を有する熱交換ライン５と、２つのタービン−ブースタ装置６および７を備える。装置６は、ブースタ８と、同じシャフト１０上に設けられた温低圧タービン９を備え、装置７は、ブースタ１１と、同じシャフト１３上に設けられた冷高圧タービン１２を備える。２つのブースタ８および１１は、直列に設けられている。   The device also comprises a heat exchange line 5 with a countercurrent circulation of fluid in heat exchange relation and two turbine-booster devices 6 and 7. The apparatus 6 includes a booster 8 and a hot / low pressure turbine 9 provided on the same shaft 10, and the apparatus 7 includes a booster 11 and a cold / high pressure turbine 12 provided on the same shaft 13. The two boosters 8 and 11 are provided in series.

圧縮機Ｃ内で約２０バール（絶対）に圧縮され、精製装置Ａでの精製により水およびＣＯ2が除去された、分離する空気を、第１のブースタ１１により約３２バール（絶対）に昇圧する。ついで、この流れを２つに分ける。この空気の第１の部分Ｐ１は、上記熱交換ラインに送り、温度Ｔ１、例えば−１２５℃のオーダーの温度まで、熱交換ライン５のダクト内で冷却する。ついで、これを、ダクト１７を介して熱交換ライン５から取り出し、タービン１２内で６バール（絶対）まで膨張させる。空気は、そのほぼ露点で、このタービンを出る。この空気の一部、例えば４分の１を、熱交換ライン１４の冷末端に達するまで冷却し続けることができる。 The air to be separated, compressed in the compressor C to about 20 bar (absolute) and from which water and CO 2 have been removed by purification in the refiner A, is boosted to about 32 bar (absolute) by the first booster 11. To do. Then this flow is divided into two. This first part P1 of air is sent to the heat exchange line and cooled in the duct of the heat exchange line 5 to a temperature T1, for example a temperature on the order of −125 ° C. This is then removed from the heat exchange line 5 via the duct 17 and expanded in the turbine 12 to 6 bar (absolute). Air exits this turbine at its near dew point. A portion of this air, for example a quarter, can continue to be cooled until the cold end of the heat exchange line 14 is reached.

上記空気の第２の部分Ｐ２は、第２のブースタ８内で、３８バールの圧力までさらに圧縮した後、ダクト１４内でその温末端（warm end）から冷末端に通じることにより冷却する。この空気は、液体状態でダクト１４を出、その後、ダクト１５を介して、膨張弁１６内で６バールまで膨張させ、高圧カラム２の底部に注入する。この液体空気は、上記低圧まで膨張させ、カラム３に注入することができる。   The second portion P2 of air is further compressed in the second booster 8 to a pressure of 38 bar and then cooled in the duct 14 by passing from its warm end to its cold end. This air exits the duct 14 in the liquid state and is then expanded to 6 bar in the expansion valve 16 via the duct 15 and injected into the bottom of the high pressure column 2. This liquid air can be expanded to the low pressure and injected into the column 3.

全ての空気（または残存空気）は３８バールにある。   All air (or residual air) is at 38 bar.

２０バール（絶対）に圧縮された初期空気流の例えば約１／１０に相当する、タービン１２からの空気の一部は、導管１８を介してカラム２のバット部分に送り、残りの部分を、熱交換ラインのダクト１９内で、この熱交換ラインの冷末端から、Ｔ１よりもはるかに高い温度Ｔ２まで温める。この温度Ｔ２は、例えば、室温〜−２０℃であり得る。   A portion of the air from the turbine 12 corresponding to, for example, about 1/10 of the initial air flow compressed to 20 bar (absolute) is sent via conduit 18 to the bat portion of the column 2 and the remaining portion is In the duct 19 of the heat exchange line, it is warmed from the cold end of this heat exchange line to a temperature T2 that is much higher than T1. This temperature T2 can be, for example, room temperature to −20 ° C.

こうして加温された空気を、ダクト２０を介して、熱交換ラインから取り出し、タービン９中でほぼ大気圧まで膨張させる。この空気は、該タービンから、Ｔ１近傍の温度で出てゆく。その後、この空気を、ダクト２１を介して熱交換ラインに再導入し、ダクト２２内で室温まで加温し、そして流入する空気を精製するために使用した吸着剤を冷却するために、および／または本装置の主圧縮機から出てゆく空気を冷却するために最終的に使用した後、当該装置から排出する。   The air thus heated is taken out from the heat exchange line via the duct 20 and expanded to almost atmospheric pressure in the turbine 9. This air exits the turbine at a temperature near T1. This air is then reintroduced into the heat exchange line via the duct 21, warmed to room temperature in the duct 22, and to cool the adsorbent used to purify the incoming air and / or Or after using finally to cool the air which leaves the main compressor of this apparatus, it exhausts from the said apparatus.

変形例として、図１に示すように、タービン９からの空気の全てを、熱交換ラインの温末端に達するまで加温し、ついで大気に排出することができる。   As a modification, as shown in FIG. 1, all of the air from the turbine 9 can be heated until reaching the warm end of the heat exchange line and then discharged to the atmosphere.

本装置のその他の部分はよく知られているものである。カラム２のバット部分に集められた富化液体ＬＲ（酸素富化空気）は、低圧カラム３の頂部から来る残存窒素を加熱することにより過冷却器（sub-cooler）２５内で過冷却した後、カラム３に送り、その後これを、膨張弁２６内で膨張させる。カラム２の上部から取り出された、実質的に窒素からなる貧液体ＬＰは、過冷却器２５内で過冷却した後、カラム３に送り、その後これを膨張弁２８内で膨張させる。本装置は、ダクト２９を介してカラム２のヘッド部分中に収集された液体窒素を生産する。液体窒素は、過冷却器２５内で過冷却され、膨張弁３０内でほぼ大気圧まで膨張させ、容器３１内に貯蔵する。ダクト３２を介してカラム３のバット部分に収集された液体酸素は、過冷却器２５内で過冷却されている。これは、ダクト３４を介してカラム３のヘッド部分に取り出された残存窒素により冷却される。カラム３の底部から取り出された気体３５の形態にある酸素は、主熱交換器により温められ、流入する空気を冷却する。カラム３の頂部から取り出されたもう一つの生成物低圧窒素３７も、過冷却器および主熱交換器を通り、他の流入するガスおよび液体を冷却する。   The other parts of the device are well known. After the enriched liquid LR (oxygen-enriched air) collected in the bat portion of the column 2 is subcooled in the sub-cooler 25 by heating the residual nitrogen coming from the top of the low pressure column 3 , Sent to the column 3, which is then expanded in the expansion valve 26. The poor liquid LP substantially consisting of nitrogen taken out from the upper part of the column 2 is supercooled in the subcooler 25 and then sent to the column 3, and then expanded in the expansion valve 28. The apparatus produces liquid nitrogen collected in the head portion of column 2 via duct 29. The liquid nitrogen is supercooled in the subcooler 25, expanded to almost atmospheric pressure in the expansion valve 30, and stored in the container 31. Liquid oxygen collected in the bat portion of the column 3 through the duct 32 is supercooled in the supercooler 25. This is cooled by the residual nitrogen taken out to the head portion of the column 3 through the duct 34. Oxygen in the form of gas 35 taken from the bottom of the column 3 is warmed by the main heat exchanger and cools the incoming air. Another product, low pressure nitrogen 37, taken from the top of column 3, also passes through the subcooler and main heat exchanger to cool other incoming gases and liquids.

本装置は、アルゴン富化供給流を低圧カラム３からアルゴンカラム３９に送るための導管３８をも備えている。アルゴンは、窒素除去カラム４１内でさらに精製される。本プロセスのこの部分は、全体として標準的なものであり、詳しくは説明しない。   The apparatus also includes a conduit 38 for sending an argon enriched feed stream from the low pressure column 3 to the argon column 39. Argon is further purified in a nitrogen removal column 41. This part of the process is generally standard and will not be described in detail.

図２において、ｘ軸は温度（℃）を示し、ｙ軸は熱流量を示す。下側の線Ｃ１は、冷却され、液化される空気の熱流量の変動を示し、上側の線Ｃ２は、加温されるガスの熱流量を示す。このことから以下のことがわかる。   In FIG. 2, the x-axis indicates temperature (° C.), and the y-axis indicates heat flow. The lower line C1 shows the variation in the heat flow of the cooled and liquefied air, and the upper line C2 shows the heat flow of the heated gas. This shows the following.

冷タービン１２は、空気の液化ゾーンを境界付ける入口温度と出口温度を有する高流量の空気を処理する。すなわち、冷タービンは、その低圧での操作にもかかわらず、多くの寒冷（cold）を生成し、さらにこの寒冷を、空気を液化するために正確に多量の冷却が必要とされ、かつ他方ヘッド損失が最大であるところの温度ゾーン中に生成させる。温タービンは、小流量の空気を処理し、６バールから１バールへの膨張を確保することにより、先の温度ゾーンの上に位置し、冷却がタービンにより確保されるところの温度ゾーンの実質部を回復（recover）する。したがって、タービン９は、広範囲の温度にわたって少量の冷却を生み出す。   The cold turbine 12 processes a high flow of air having an inlet temperature and an outlet temperature that bound the air liquefaction zone. That is, a cold turbine produces a lot of cold despite its low pressure operation, and this cold requires an exact amount of cooling to liquefy the air and the other head It is generated in the temperature zone where the loss is greatest. The hot turbine is located above the previous temperature zone by treating a small flow of air and ensuring expansion from 6 bar to 1 bar, the substantial part of the temperature zone where cooling is ensured by the turbine. Recover. Thus, the turbine 9 produces a small amount of cooling over a wide range of temperatures.

上記考察から、図１の装置は減少した液化の比エネルギーをもたらすことがわかる。また、ダクト１８内を循環する高圧空気は、不都合なく、その露点近傍にあり、これは、二重カラムにおける蒸留に重要である。   From the above considerations, it can be seen that the apparatus of FIG. 1 provides a reduced specific energy of liquefaction. Also, the high pressure air circulating in the duct 18 is inconveniently near its dew point, which is important for distillation in a double column.

本発明により空気を蒸留するための装置の概略図。1 is a schematic view of an apparatus for distilling air according to the present invention. 本発明による液化サイクルの熱交換ダイアグラム。2 is a heat exchange diagram of a liquefaction cycle according to the present invention.

符号の説明Explanation of symbols

１…二重カラム
２…高圧カラム
３…低圧カラム
４…気化器−凝縮器
５，１４…熱交換ライン
６，７…タービン−ブースタ装置
８，１１…ブースタ
９…温低圧タービン
１０，１３…シャフト
１２…冷高圧タービン
１５，１７，２０，２１，２２，２９，３２，３４…ダクト
１６，２６，２８，３０…膨張弁
１８…導管
２５…過冷却器
３１…容器
３５…気体酸素
３７…低圧窒素
３８…アルゴンカラム
４１…窒素除去カラム DESCRIPTION OF SYMBOLS 1 ... Double column 2 ... High pressure column 3 ... Low pressure column 4 ... Vaporizer-condenser 5,14 ... Heat exchange line 6,7 ... Turbine-booster device 8,11 ... Booster 9 ... Warm and low pressure turbine 10,13 ... Shaft DESCRIPTION OF SYMBOLS 12 ... Cold high pressure turbine 15, 17, 20, 21, 22, 29, 32, 34 ... Duct 16, 26, 28, 30 ... Expansion valve 18 ... Conduit 25 ... Subcooler 31 ... Container 35 ... Gaseous oxygen 37 ... Low pressure Nitrogen 38 ... Argon column 41 ... Nitrogen removal column

Claims (7)

高圧カラム（２）と低圧カラム（３）を備える二重カラム（１）を少なくとも備える低温蒸留装置を用いる低温蒸留により空気を分離するための方法であって、空気を圧縮機中で第１の圧力に圧縮し、冷却し、および精製し、前記第１の圧力にある空気を第１および第２のブースタ圧縮機（１１、８）中で第２の圧力に圧縮した後、熱交換器（５）中で冷却し、前記熱交換器に送られた前記第２の圧力にある空気（１５）の少なくとも一部を冷却し、液化し、および前記二重カラムの少なくとも１つのカラムに送り、該空気の少なくとも一部を、前記第１のブースタ圧縮機中で、前記第１の圧力と第２の圧力の中間の圧力に圧縮し、冷却し、および第１の入口温度を有する第１のタービン（１２）中で膨張させ、前記第１のタービン中で膨張された空気の第１の部分を前記高圧カラムに送り、前記第１のタービン中で膨張された空気の第２の部分（１９）を加温すべく前記熱交換器に送り、この加温された空気の第２の部分を、第２のタービン（９）中で膨張させ、前記熱交換器に戻し、さらに加温する該方法。   A method for separating air by low temperature distillation using a low temperature distillation apparatus comprising at least a double column (1) comprising a high pressure column (2) and a low pressure column (3), wherein the air is first in a compressor. After compressing to pressure, cooling and purifying and compressing the air at said first pressure to a second pressure in first and second booster compressors (11, 8), a heat exchanger ( 5) Cool in, cool at least a portion of the air (15) at the second pressure sent to the heat exchanger, liquefy and send to at least one column of the double column; At least a portion of the air is compressed in the first booster compressor to a pressure intermediate between the first pressure and the second pressure, cooled, and having a first inlet temperature; Expanded in turbine (12) and expanded in said first turbine A first portion of the air that has been sent to the high pressure column, and a second portion (19) of the air that has been expanded in the first turbine is sent to the heat exchanger to be heated and heated. The method wherein the second part of the heated air is expanded in a second turbine (9), returned to the heat exchanger and further heated. 前記中間の圧力に圧縮され、さらに圧縮することなく冷却された全ての空気を前記第１のタービン（１２）に送る請求項１に記載の方法。   The method of claim 1, wherein all air compressed to the intermediate pressure and cooled without further compression is sent to the first turbine (12). 少なくとも１種の液体生成物が製造される請求項１または２に記載の方法。   The process according to claim 1 or 2, wherein at least one liquid product is produced. 前記第１のブースタ圧縮機（１１）が、前記第１のタービン（１２）に連結され、前記第２のブースタ圧縮機（８）が、前記第２のタービン（９）に連結されている請求項１〜３のいずれか１項に記載の方法。   The first booster compressor (11) is connected to the first turbine (12) and the second booster compressor (8) is connected to the second turbine (9). Item 4. The method according to any one of Items 1 to 3. 高圧カラム（２）と低圧カラム（３）を備える二重カラム（１）、圧縮機（Ｃ）、第１および第２のタービン（１２、９）、第１および第２のブースタ圧縮機（１１、８）、熱交換器（５）、第１の圧力にある空気を、前記圧縮機から、直列に接続された前記第１および第２のブースタ圧縮機に送るための手段、第２の圧力にある空気を、前記第２のブースタ圧縮機の出口から、前記熱交換器に送り、ついで前記二重カラムの少なくとも１つのカラムに送るための手段、前記第１のブースタ圧縮機から空気を取り出すための手段、前記第１のブースタ圧縮機から取り出された空気を前記熱交換器に送り、ついで前記第１のタービンに送るための手段、前記第１のタービンから空気を前記高圧カラムに送るための手段、前記第１のタービンから空気を熱交換器の冷末端に送るための手段、前記第１のタービンから前記熱交換器に送られた空気を前記熱交換器の中間点から取り出すための手段、該取り出された空気を第２のタービンに送るための手段、並びに前記第２のタービンから空気を前記熱交換器へ戻すための手段を備える、低温蒸留により空気を分離するための装置。   Double column (1) comprising a high pressure column (2) and a low pressure column (3), compressor (C), first and second turbines (12, 9), first and second booster compressors (11 8), heat exchanger (5), means for sending air at a first pressure from the compressor to the first and second booster compressors connected in series, a second pressure Means for sending air from the outlet of the second booster compressor to the heat exchanger and then to at least one column of the double column, taking air from the first booster compressor Means for sending air taken from the first booster compressor to the heat exchanger and then to the first turbine, for sending air from the first turbine to the high pressure column Means from the first turbine Means for sending air to the cold end of the heat exchanger, means for removing air sent from the first turbine to the heat exchanger from an intermediate point of the heat exchanger, and An apparatus for separating air by cryogenic distillation comprising means for sending to a second turbine and means for returning air from the second turbine to the heat exchanger. 前記第１のブースタ圧縮機の出口が、前記第１のタービンの入口のみに接続されている請求項５に記載の装置。   The apparatus of claim 5, wherein an outlet of the first booster compressor is connected only to an inlet of the first turbine. 前記第１のブースタ圧縮機（１１）が、前記第１のタービン（１２）に連結され、前記第２のブースタ圧縮機（８）が、前記第２のタービン（９）に連結されている請求項５または６に記載の装置。   The first booster compressor (11) is connected to the first turbine (12) and the second booster compressor (8) is connected to the second turbine (9). Item 7. The device according to Item 5 or 6.
JP2006139954A 2005-05-20 2006-05-19 Method and device for separating air by low temperature distillation Pending JP2006329615A (en)

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