JP3180832U - Equipment for the production of pressurized purified air and liquid products by cryogenic distillation - Google Patents

Equipment for the production of pressurized purified air and liquid products by cryogenic distillation Download PDF

Info

Publication number
JP3180832U
JP3180832U JP2012006542U JP2012006542U JP3180832U JP 3180832 U JP3180832 U JP 3180832U JP 2012006542 U JP2012006542 U JP 2012006542U JP 2012006542 U JP2012006542 U JP 2012006542U JP 3180832 U JP3180832 U JP 3180832U
Authority
JP
Japan
Prior art keywords
pressure
fraction
column
liquid
conduit
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
JP2012006542U
Other languages
Japanese (ja)
Inventor
フレデリック・ボンヌ
アレン・ギヤール
ラサ・ジョアン
パトリック・ル・ボ
一考 津田
Original Assignee
レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード filed Critical レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード
Application granted granted Critical
Publication of JP3180832U publication Critical patent/JP3180832U/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04066—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • 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
    • 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
    • F25J3/04321—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 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
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04363—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of 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
    • 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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • 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
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2250/10—Boiler-condenser with superposed stages
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

【課題】空気の低温蒸留によって、加圧された精製された空気と液体生成物の製造のための装置を提供する。
【解決手段】第１のカラムＡに塔頂コンデンサＣを備える蒸留カラムシステムと、熱交換器９と、タービンと、空気を第１の圧力に圧縮するためのコンプレッサＶと、前記第１の圧力で空気を精製するための精製手段Ｐと、前記第１の圧力で前記精製された空気を第１の分留と第２の分留とに分けるための導管手段と、複数の導管とを具備する。
【選択図】図１An apparatus for the production of pressurized purified air and liquid products by cryogenic distillation of air.
A distillation column system having a top condenser C in a first column A, a heat exchanger 9, a turbine, a compressor V for compressing air to a first pressure, and the first pressure. Purification means P for purifying air, conduit means for separating the purified air at the first pressure into a first fraction and a second fraction, and a plurality of conduits To do.
[Selection] Figure 1

Description

この発明は、低温蒸留による、加圧された精製された空気と液体生成物の製造のための装置と方法とに関する。   This invention relates to an apparatus and method for the production of pressurized purified air and liquid products by cryogenic distillation.

エネルギを産出するために、タービン内で、圧縮された空気を精製して、精製された空気を膨張させることによって清潔な乾燥した空気を製造することは、ＥＰ−Ａ−１０２７９１３から知られている。   It is known from EP-A-1027913 to produce clean dry air by purifying compressed air and expanding the purified air in a turbine to produce energy. .

この発明は、液体生成物を製造するために、精製された加圧された空気の膨張により作り出された冷却を用いる。膨張された空気が大気に送られるケースとは逆に、このケースでは、膨張された空気は、少なくとも３絶対バール（３ bar abs ）、好ましくは５絶対（５ bar abs）の気圧で、除去される。なぜなら、それは、純粋な空気の生成物として機能するつもりだからである。   This invention uses the cooling created by the expansion of purified pressurized air to produce a liquid product. In contrast to the case where the expanded air is sent to the atmosphere, in this case, the expanded air is removed at a pressure of at least 3 absolute bar (3 bar abs), preferably 5 absolute (5 bar abs). The Because it intends to function as a product of pure air.

この発明によると、空気の低温蒸留による、加圧された精製された空気と液体生成物との製造のための方法が提供される。この中では、
ｉ）空気は、第１の圧力に圧縮され、前記第１の圧力で精製された空気を作るために精製され、
ｉｉ）前記第１の圧力の前記精製された空気は、第１の留分（fraction）と、第２の留分とに分けられ、
ｉｉｉ）前記第１の留分は、熱交換器内で冷却されて蒸留カラムシステムの第１のカラムに送られ、
ｉｖ）前記第２の留分は、前記熱交換器内で中間温度（intermediate temperature）に冷却され、前記第１の圧力から前記第２の圧力まで膨張され、前記熱交換器内で前記第２の圧力で暖められ、生成物の流れ（product stream）として取り除かれ、
ｖ）前記第１の圧力は、前記第２の圧力よりも少なくとも３バール（bars） 高く、前記第２の圧力は、３絶対バール（３ bars abs）よりも大きく、
ｖｉ）前記第１のカラムからの酸素が豊富にされた液体（oxygen enriched liquid）は、塔頂コンデンサ（top condenser）内で気化され、第１の酸素が豊富にされたガスとして取り除かれ、
ｖｉｉ）窒素が豊富にされた流体（nitrogen enriched fluid）は、前記第１のカラムから取り除かれ、
ｖｉｉｉ）少なくとも１つの液体生成物は、前記蒸留カラムシステムから取り除かれる。 According to this invention, a process is provided for the production of pressurized purified air and liquid products by cryogenic distillation of air. In this,
i) air is compressed to a first pressure and purified to produce air purified at said first pressure;
ii) the purified air at the first pressure is divided into a first fraction and a second fraction;
iii) the first fraction is cooled in a heat exchanger and sent to the first column of the distillation column system;
iv) The second fraction is cooled to an intermediate temperature in the heat exchanger, expanded from the first pressure to the second pressure, and the second fraction in the heat exchanger. Heated at a pressure of, removed as a product stream,
v) the first pressure is at least 3 bars higher than the second pressure, and the second pressure is greater than 3 bars abs;
vi) Oxygen enriched liquid from the first column is vaporized in a top condenser and removed as a first oxygen enriched gas;
vii) a nitrogen enriched fluid is removed from the first column;
viii) At least one liquid product is removed from the distillation column system.

任意に：
― 少なくとも１つの液体生成物は、前記第１のカラムから取り除かれた液体窒素である。 Arbitrarily:
The at least one liquid product is liquid nitrogen removed from the first column.

― 前記第１の酸素が豊富にされたガスは、圧縮されて前記第１のカラムに戻される。 The gas enriched in the first oxygen is compressed and returned to the first column;

― 酸素が豊富な液体は、蒸留カラムシステムの前記第１のカラムの塔頂コンデンサから取り除かれて第２のカラムの塔頂に送られ、前記酸素が豊富にされた液体は、前記第２のカラムの塔底から液体生成物として取り除かれる。 The oxygen rich liquid is removed from the top condenser of the first column of the distillation column system and sent to the top of the second column, and the oxygen enriched liquid is It is removed as a liquid product from the bottom of the column.

― 前記第１のカラムのコンデンサからの酸素が豊富にされたガスは、タービン内で膨張される。 The oxygen enriched gas from the first column condenser is expanded in a turbine.

この発明の他の側面によると、空気の低温蒸留による、加圧された精製された空気と液体生成物の製造のための装置が提供される。この装置は、少なくとも１つの塔頂コンデンサを備える少なくとも第１のカラムを備える蒸留カラムシステムと、熱交換器と、タービンと、第１の圧力に圧縮するためのコンプレッサと、第１の圧力で空気を精製するための精製手段と、前記第１の圧力で前記精製された空気を第１の分留（fraction）と第２の分留（fraction）とに分ける導管手段（conduits means）と、前記熱交換器内で冷却されるべき前記第１の留分を送るための導管（conduit）と、蒸留カラムシステムの前記第１のカラムに、前記熱交換器で冷却された前記第１の留分を送る導管と、前記熱交換器内で中間温度に冷却されるべき前記第２の留分を送るための導管と、前記中間温度の前記第２の留分を前記熱交換器内から取り除くための、かつ、前記第１の圧力で前記第２の留分をタービンに送るための導管と、前記第２の圧力の膨張された、前記熱交換器内で前記第２の圧力で昇温されるべき前記第２の留分を前記第２の圧力で送るための導管と、前記生成物流れとして昇温された前記第２の留分を第２の圧力で取り除くための導管とを具備し、前記第１の圧力は、前記第２の圧力よりも少なくとも３バール高く、前記第２の圧力は、３絶対バール（３ bars abs）よりも大きい。そして、前記第１のカラムからの酸素が豊富にされた液体が、前記第１のカラムの１つの前記塔頂コンデンサ内で気化されるために送るための導管と、前記気化された酸素が豊富にされた液体を、第１の酸素が豊富にされたガスとして取り除くための導管と、前記第１のカラムから窒素が豊富にされた流体を取り除くための導管と、前記蒸留カラムシステムから少なくとも１つの液体生成物を取り除くための導管とを具備する。   According to another aspect of the invention, there is provided an apparatus for the production of pressurized purified air and liquid products by cryogenic distillation of air. The apparatus includes a distillation column system comprising at least a first column comprising at least one overhead condenser, a heat exchanger, a turbine, a compressor for compressing to a first pressure, and air at a first pressure. A purification means for purifying the gas; conduit means for dividing the purified air at the first pressure into a first fraction and a second fraction; and A conduit for sending the first fraction to be cooled in a heat exchanger, and the first fraction cooled in the heat exchanger to the first column of a distillation column system; A conduit for delivering the second fraction to be cooled to an intermediate temperature in the heat exchanger, and for removing the second fraction at the intermediate temperature from within the heat exchanger. Of the second fraction at the first pressure. A conduit for sending to the bin and the second fraction to be heated at the second pressure in the heat exchanger expanded at the second pressure at the second pressure. And a conduit for removing the second fraction heated as the product stream at a second pressure, wherein the first pressure is at least 3 than the second pressure. The bar is high and the second pressure is greater than 3 bars abs. And a conduit for sending the oxygen enriched liquid from the first column to be vaporized in one overhead condenser of the first column, and the vaporized oxygen enriched At least one from the distillation column system, a conduit for removing the liquefied liquid as a first oxygen-enriched gas, a conduit for removing the nitrogen-enriched fluid from the first column, And a conduit for removing one liquid product.

任意に、装置は、第２の蒸留カラムと、手段とを備える。この手段は、第２の蒸留カラムシステムに、第１のカラムまたは前記塔頂コンデンサから、または、前記第１のカラムと前記塔頂コンデンサとから、酸素が豊富にされた液体を与えるための手段である。   Optionally, the apparatus comprises a second distillation column and means. Means for providing a second distillation column system with a liquid enriched in oxygen from the first column or the overhead condenser, or from the first column and the overhead condenser. It is.

最も少ない１つ（the least one）の液体生成物は、液体窒素と液体酸素との少なくともの一方を備えてもよい。   The least one liquid product may comprise at least one of liquid nitrogen and liquid oxygen.

この発明は、この発明の方法を示す図面を参照してより詳しく説明される。   The invention will be explained in more detail with reference to the drawings showing the method of the invention.

図１は、この発明の最も簡単な形態を示している。図１中では、コンプレッサＶ内で９〜１０バールの第１の圧力に圧縮される空気１は、精製ユニットＰ内で水と二酸化炭素とを取り除くために精製され、第１の分留５と第２の分留３とに分けられる。第１の分留５は、真鍮がかぶせられた（brazed）アルミニウムの熱交換器９内で完全に冷却され、１つのカラム窒素蒸留システムに送られる。カラムＡは、酸素が豊富にされた液体１１を形成する酸素を塔底で分離し、窒素が豊富なガスを塔頂で分離する。窒素が豊富なガスは、塔頂コンデンサＣ内で凝縮され、逆流としてカラムに送り戻される。酸素が豊富にされた液体１１は、その後熱交換器９内で昇温される気化された液体１５を形成するために膨張され、塔頂コンデンサＣに送られる。液体窒素１３は、生成物として取り除かれ、ガス状の窒素１７は、好ましくは生成物として、熱交換器内で昇温されるために、取り除かれる。   FIG. 1 shows the simplest form of the present invention. In FIG. 1, the air 1 compressed in the compressor V to a first pressure of 9-10 bar is purified in the purification unit P to remove water and carbon dioxide, and the first fraction 5 The second fraction 3 is divided. The first fraction 5 is completely cooled in a brassed aluminum heat exchanger 9 and sent to a single column nitrogen distillation system. Column A separates the oxygen that forms oxygen-rich liquid 11 at the bottom and separates the nitrogen-rich gas at the top. The nitrogen-rich gas is condensed in the top condenser C and sent back to the column as a reverse flow. The oxygen enriched liquid 11 is then expanded to form a vaporized liquid 15 that is heated in the heat exchanger 9 and sent to the top condenser C. Liquid nitrogen 13 is removed as a product, and gaseous nitrogen 17 is removed, preferably as a product, to be heated in a heat exchanger.

第２の分留３は、交換器９の中間温度に冷却され、タービン７内で９〜１０バールから５バールまで下げられて膨張され、５バールで昇温されるために交換器９に送り戻される。昇温された空気４は、５バールの清潔な空気生成物を構成する。   The second fraction 3 is cooled to the intermediate temperature of the exchanger 9 and expanded in the turbine 7 from 9-10 bar to 5 bar, expanded and heated to 5 bar and sent to the exchanger 9 Returned. The heated air 4 constitutes a clean air product of 5 bar.

図２では、窒素カラムは、少しばかりより複雑であり、２つの塔頂コンデンサＣ１,Ｃ２を備え、工程は、冷却コンプレッサ２５（cold compressor 25）と、不用（waste）のタービン２３とを使用する。   In FIG. 2, the nitrogen column is a little more complex and comprises two top condensers C1, C2, and the process uses a cold compressor 25 and a waste turbine 23. .

図２では、９〜１０バールの圧力に圧縮されて、精製ユニット（図示せず）で精製された空気１は、第１の分留５と第２の分留３とに分けられる。第１の分留５は、真鍮がかぶせられた（brazed）熱交換器９内で完全に冷却され一つのカラム窒素蒸留システムに送られる。カラムＡは、酸素が豊富な液体１１を形成する空気１を塔底で分離し、窒素が豊富なガスを塔頂で分離するために使用される。   In FIG. 2, the air 1 compressed to a pressure of 9-10 bar and purified in a purification unit (not shown) is divided into a first fraction 5 and a second fraction 3. The first fraction 5 is completely cooled in a brass-heated heat exchanger 9 and sent to one column nitrogen distillation system. Column A is used to separate the air 1 forming the oxygen rich liquid 11 at the bottom and the nitrogen rich gas at the top.

窒素が豊富なガスは、塔頂コンデンサＣ１,Ｃ２内で圧縮され、カラムに逆流（reflux）として送り戻される。その後冷間コンプレッサ２５内で圧縮されてカラムＡに送られる気化された液体１５を形成するために、酸素が豊富にされた液体１１は、膨張されて塔頂コンデンサＣ１に送られる。コンデンサＣ１からの液体は、下方のコンデンサＣ２に送られ、製造された（produced）気化されたガス２１は、タービン２３内で膨張され熱交換器９内で昇温される。液体窒素１３は、生成物として取り除かれ、ガス状の窒素１７は、好ましくは生成物として、交換器９内で昇温されるために取り除かれる。   The nitrogen-rich gas is compressed in the top condensers C1, C2 and sent back to the column as a reflux. The oxygen rich liquid 11 is then expanded and sent to the top condenser C1 to form a vaporized liquid 15 that is then compressed in the cold compressor 25 and sent to the column A. The liquid from the condenser C1 is sent to the lower condenser C2, and the produced vaporized gas 21 is expanded in the turbine 23 and heated in the heat exchanger 9. The liquid nitrogen 13 is removed as a product, and the gaseous nitrogen 17 is removed as it is heated in the exchanger 9, preferably as a product.

第２の空気分留３は、交換器９の中間温度に冷却され、タービン７内で９〜１０バールから５バールまで膨張され、５バールで昇温されるために交換器９に送り戻される。昇温
された空気４は、５バールの清潔な空気を構成する。 The second air fraction 3 is cooled to the intermediate temperature of the exchanger 9, expanded in the turbine 7 from 9-10 bar to 5 bar, and sent back to the exchanger 9 to be heated up at 5 bar. . The heated air 4 constitutes 5 bar of clean air.

図３は、２００ｐｐｂ酸素純度で、８．５ゲートバール（bars g）で４３０００Ｎｍ３／ｈのガス状窒素生成物流量１７と、４０００Ｎｍ３／ｈの液体窒素流量１３とを有する窒素発生装置を示している。   FIG. 3 shows a nitrogen generator with 200 ppb oxygen purity and a gaseous nitrogen product flow rate 17 of 43000 Nm 3 / h at 8.5 gate bars and a liquid nitrogen flow rate 13 of 4000 Nm 3 / h. .

８４０００Ｎｍ３／ｈで９ゲートバール（bars g）で３０℃である精製ユニットからの乾燥しており清潔な大気中の空気流れ５（Ｈ２ＯとＣＯ２とが略ない）は、第１の蒸留カラムＡの中間ステージに入る前に交換器９内で−１６４℃の温度に冷却される。 A dry and clean atmospheric air stream 5 (abbreviated H 2 O and CO 2 ) from a purification unit at 84000 Nm 3 / h at 9 gbars and 30 ° C. is the first distillation Before entering the intermediate stage of column A, it is cooled in the exchanger 9 to a temperature of −164 ° C.

１３６０００Ｎｍ３／ｈで、９．０ゲートバール（bars g）で３０℃である、乾燥しており清潔な大気中の空気流れ３（Ｈ２ＯとＣＯ２とが略ない）は、交換器９内で−１５３．５℃の温度に冷却され、流れ４としてタービン７で４ゲートバール（bars g）で−１７４℃に膨張される。この流れ４は、メイン変換器９内に入り、ここで、２８℃に昇温され、加圧生成物の圧縮乾燥空気（Compressed Dry Air pressurized product）（以下、ＣＤＡと表される）として、搬送される
タービン７で発生されるエネルギは、発生装置で回復(recover)される。 A dry and clean atmospheric air stream 3 (substantially free of H 2 O and CO 2 ) at 136000 Nm 3 / h, 9.0 ° C. at bars g is 30 ° C. Is cooled to a temperature of −153.5 ° C. and is expanded as stream 4 in turbine 7 to −174 ° C. at 4 gate bars. This stream 4 enters the main converter 9, where it is heated to 28 ° C. and conveyed as compressed product compressed air (hereinafter referred to as CDA). The energy generated in the turbine 7 is recovered by the generator.

３７％ｍｏｌ．の酸素を含み７８０００Ｎｍ３／ｈの酸素が豊富にされた液体流量１１は、窒素蒸留カラムＡの塔底から回収されて、２つの流れ（流れ１１Ａと流れ１１Ｂ）とに分けられる。   37% mol. The liquid flow rate 11 enriched with 78000 Nm 3 / h of oxygen is recovered from the bottom of the nitrogen distillation column A and divided into two streams (stream 11A and stream 11B).

４７０００Ｎｍ３／ｈの酸素が豊富な液体流量１１Ａは、バルブを横切って膨張されて、窒素蒸留カラムＡの塔頂コンデンサＣ１に供給される。   A liquid flow 11A rich in oxygen of 47000 Nm3 / h is expanded across the valve and fed to the top condenser C1 of the nitrogen distillation column A.

３１０００Ｎｍ３／ｈの酸素が豊富にされた液体流量１１Ｂ（流れ１９）は、第２の蒸留カラムＢのための再煮沸器Ｒ（reboiler）の熱源（source）として使用され、流れ１１Ａに混ぜられ、窒素蒸留カラムＡの塔頂に供給される。   A liquid flow 11B enriched in oxygen of 31000 Nm 3 / h (stream 19) is used as the heat source of the reboiler R for the second distillation column B and is mixed into the stream 11A, It is fed to the top of the nitrogen distillation column A.

２７％の酸素を有して４１０００Ｎｍ３／ｈの流量を有する、ガス状の酸素が豊富にされた再循環流れ２７は、４．７ゲートバール（bars g）で−１７２℃の窒素蒸留カラムＡの塔頂コンデンサＣ１から出て、再循環ブースタ２５内で８．９ゲートバール（bars g）に圧縮され、その後、変換器９内で−１６４．５℃に過冷却（subcooled）され蒸留カラムＡの下部のステージに供給される。   Gaseous oxygen-enriched recycle stream 27 with 27% oxygen and a flow rate of 41000 Nm 3 / h was applied to nitrogen distillation column A at −172 ° C. at 4.7 gate bars (bars g). From the top condenser C1, it is compressed in the recycle booster 25 to 8.9 gates bar and then subcooled in the converter 9 to -164.5 ° C. Supplied to the lower stage.

３１１００Ｎｍ３／ｈで３．７ゲートバール（bars g）で−１７２℃のコンデンサＣ２からのガス状の酸素が豊富な廃物（waste）２１は、交換器９内で−１３５℃に昇温され、タービン２３内で膨張され、メイン交換器９内に再び入り、２８℃に昇温される。   Gaseous oxygen-rich waste 21 from condenser C2 at −172 ° C. with 3.7 gate bars at 31100 Nm 3 / h is raised to −135 ° C. in the exchanger 9 and is It is expanded in 23, enters the main exchanger 9 again, and is heated to 28 ° C.

タービン２３は、冷却ブースタ２５に連結される。   The turbine 23 is connected to the cooling booster 25.

廃物流れ２１（waste stream 21）は、３５３８０Ｎｍ３／ｈの流量（flow）と、４５．２％の酸素とを備え、
６８％の酸素を含み５９００Ｎｍ３／ｈの酸素が豊富な液体流量１５は、塔頂コンデンサＣ２から、バルブを通って膨張した後、酸素蒸留カラムＢに供給される。 Waste stream 21 comprises a flow of 35380 Nm3 / h and 45.2% oxygen,
A liquid flow rate 15 containing 68% oxygen and rich in 5900 Nm 3 / h oxygen is supplied from the top condenser C 2 to the oxygen distillation column B after being expanded through a valve.

４２８０Ｎｍ３／ｈの流量（flow）を有し、５６．１％の酸素を含む廃物ガス流れ（waste gas stream ）２８は、０．５ゲートバール（bar g） で−１８３℃で酸素蒸留カラムＢの上部から出て、メイン変換器９内で２８℃に昇温される。   A waste gas stream 28 having a flow of 4280 Nm3 / h and containing 56.1% oxygen is at -183 ° C. at 0.5 gate bar (bar g). From the top, the temperature is raised to 28 ° C. in the main converter 9.

蒸留カラムＢの排水だめ（sump）Ｏ２から、１６２０Ｎｍ３／ｈの液体酸素流量２９は、生成物として取り出される。   From the sump O2 of the distillation column B, a liquid oxygen flow rate 29 of 1620 Nm3 / h is withdrawn as product.

図４は、図３に対して、２つの冷却ブースタ２３Ａ,２３Ｂと、２つのタービン２５Ａ，２５Ｂが使用されることが異なる。酸素が豊富にされた流れ２１は、流れ２１Ａ，２１Ｂに分けられ、流れ２１Ａ，２１Ｂの各々は、タービン２３Ａ，２３Ｂの１つに送られる。酸素が豊富にされた流れ２７は、流れ２７Ａ，２７Ｂに分けられ、流れ２７Ａ，２７Ｂの各々は、冷却コンプレッサ２３Ａ，２３Ｂの１つに送られる。膨張された流れは、混合されて熱交換器内で昇温され、圧縮された流れは、混合されて過冷却された後カラムＡに送られる。   FIG. 4 differs from FIG. 3 in that two cooling boosters 23A and 23B and two turbines 25A and 25B are used. Oxygen rich stream 21 is split into streams 21A and 21B, each of streams 21A and 21B being sent to one of turbines 23A and 23B. Oxygen rich stream 27 is split into streams 27A and 27B, each of streams 27A and 27B being sent to one of cooling compressors 23A and 23B. The expanded stream is mixed and heated in the heat exchanger, and the compressed stream is mixed and subcooled and then sent to the column A.

［付記１］
ｉ）空気が、第１の圧力に圧縮されて、精製された空気を形成するために第１の圧力で精製され、
ｉｉ）前記第１の圧力の精製された空気は、第１の分留と第２の分留とに分けられ、
ｉｉｉ）前記第１の分留は、熱交換器（９）内で冷却されて、蒸留カラムシステムの第１のカラム（Ａ）に送られ、
ｉｖ）第２の分留は、前記熱交換器内で中間温度（intermediate temperature）に冷却され、前記第１の圧力から第２の圧力に膨張され、前記熱交換器内で第２の圧力で昇温され、生成物流れとして取り除かれ、
ｖ）前記第１の圧力は、前記第２の圧力よりも少なくても３バール高く、前記第２の圧力は、３絶対バール（３ bars abs）よりも大きく、
ｖｉ）前記第１のカラムからの酸素が豊富にされた液体は、第１のカラムの塔頂コンデンサ（Ｃ，Ｃ１，Ｃ２）内で気化され、第１の酸素が豊富にされたガスとして取り除かれ、
ｖｉｉ）窒素が豊富にされた流体は、第１のカラムから取り除かれ、
ｖｉｉｉ）少なくとも１つの液体生成物が、前記蒸留カラムシステムから取り除かれる
ことを特徴とする、空気の低温蒸留によって、加圧された精製された空気と液体生成物の製造のための方法。 [Appendix 1]
i) the air is compressed to a first pressure and purified at a first pressure to form purified air;
ii) the purified air at the first pressure is divided into a first fraction and a second fraction;
iii) the first fraction is cooled in a heat exchanger (9) and sent to the first column (A) of the distillation column system;
iv) The second fractionation is cooled to an intermediate temperature in the heat exchanger, expanded from the first pressure to a second pressure, and at a second pressure in the heat exchanger. Heated up and removed as product stream,
v) the first pressure is at least 3 bar higher than the second pressure, the second pressure is greater than 3 bars abs;
vi) The liquid enriched in oxygen from the first column is vaporized in the top condenser (C, C1, C2) of the first column and removed as a gas enriched in the first oxygen. And
vii) the nitrogen enriched fluid is removed from the first column;
viii) A process for the production of pressurized purified air and liquid product by cryogenic distillation of air, characterized in that at least one liquid product is removed from the distillation column system.

［付記２］
少なくとも１つの液体生成物は、前記第１のカラム（Ａ）から取り除かれた液体窒素である
ことを特徴とする付記１に記載の方法。 [Appendix 2]
The method of claim 1, wherein the at least one liquid product is liquid nitrogen removed from the first column (A).

［付記３］
前記第１の酸素が豊富にされたガス（２７）は、圧縮され、第１のカラムに送り戻される
ことを特徴とする付記１または２に記載の方法。 [Appendix 3]
The method according to claim 1 or 2, wherein the first oxygen-enriched gas (27) is compressed and sent back to the first column.

［付記４］
酸素が豊富にされた液体は、第１のカラムの塔頂コンデンサ（Ｃ２）から取り除かれ、蒸留カラムシステムの第２のカラム（Ｂ）の塔頂に送られ、酸素が豊富な液体（２９）は、第２のカラムの塔底から液体生成物として取り除かれる
ことを特徴とする付記１〜３のうちのいずれか１つに記載の方法。 [Appendix 4]
The oxygen enriched liquid is removed from the top condenser (C2) of the first column and sent to the top of the second column (B) of the distillation column system to provide an oxygen rich liquid (29). Is removed from the bottom of the second column as a liquid product. The method according to any one of appendices 1-3.

［付記５］
前記第１のカラム（Ａ）のコンデンサ（Ｃ２）からの、酸素が豊富にされたガスは、タービン（２３）内で膨張される
ことを特徴とする付記１〜４のうちのいずれか１つに記載の方法。 [Appendix 5]
Any one of appendices 1-4, wherein the oxygen-enriched gas from the condenser (C2) of the first column (A) is expanded in a turbine (23). The method described in 1.

図１は、この発明の最も簡単な形態を示す図である。FIG. 1 is a diagram showing the simplest form of the present invention. 図２は、少しばかりより複雑な窒素カラムを示す図である。FIG. 2 shows a slightly more complicated nitrogen column. 図３は、窒素発生装置を示す図である。FIG. 3 is a diagram showing a nitrogen generator. 図４は、２つの冷却ブースタと、２つのタービンが使用される図である。 FIG. 4 shows the use of two cooling boosters and two turbines .

Claims (3)

少なくとも第１のカラム（Ａ）を備え、前記第１のカラム（Ａ）は少なくとも１つの塔頂コンデンサ（Ｃ，Ｃ１，Ｃ２）を備える蒸留カラムシステムと、熱交換器（９）と、タービン（２３）と、空気を第１の圧力に圧縮するためのコンプレッサ（Ｖ）と、前記第１の圧力で空気を精製するための精製手段（Ｐ）と、前記第１の圧力で前記精製された空気を第１の分留（fraction）と第２の分留（fraction）とに分けるための導管手段と、前記熱交換器内で冷却されるべき前記第１の分留を送るための導管と、前記熱交換器内で冷却された前記第１の分留を、蒸留カラムシステムの前記第１のカラムに送るための導管と、前記熱交換器内で中間温度に冷却されるべき前記第２の分留を送るための導管と、前記第２の分留を前記熱交換器から前記中間温度で第２の分留を取り除くための、かつ、前記第１の圧力で前記第２の分留を前記タービンに送るための導管と、前記熱交換器内で第２の圧力で膨張された昇温されるべき前記第２の分留を、前記第２の圧力で送るための導管と、前記昇温された第２の分留を、前記第２の圧力で生成物流れとして取り除くための導管とを具備し、前記第１の圧力は、第２の圧力よりも少なくとも３バール（bars）高く、前記第２の圧力は、３絶対バール（bars abs）よりも大きく、そして前記第１のカラムからの酸素が豊富にされた液体が、前記第１のカラムの１つの前記塔頂コンデンサ内で気化されるために送るための導管と、気化された酸素が豊富にされた液体を、第１の酸素が豊富にされたガスとして取り除くための導管と、第１のカラムから窒素が豊富にされた流体を取り除くための導管と、蒸留カラムシステムから少なくとも１つの液体生成物を取り除くための導管とを具備する
ことを特徴とする、空気の低温蒸留によって、加圧された精製された空気と液体生成物の製造のための装置。 A distillation column system comprising at least a first column (A), said first column (A) comprising at least one overhead condenser (C, C1, C2), a heat exchanger (9), a turbine ( 23), a compressor (V) for compressing air to a first pressure, a purification means (P) for purifying air at the first pressure, and the purified at the first pressure Conduit means for dividing air into a first fraction and a second fraction; and a conduit for sending the first fraction to be cooled in the heat exchanger; A conduit for sending the first fraction that has been cooled in the heat exchanger to the first column of a distillation column system; and the second to be cooled to an intermediate temperature in the heat exchanger. A conduit for sending a fraction of the second fraction, and the second fraction from the heat exchanger to the intermediate A conduit for removing the second fraction at temperature and for sending the second fraction to the turbine at the first pressure, and expanded at the second pressure in the heat exchanger; A conduit for sending the second fraction to be heated at the second pressure and for removing the elevated second fraction as a product stream at the second pressure And wherein the first pressure is at least 3 bars higher than the second pressure, the second pressure is greater than 3 absolute bars, and the first pressure A conduit for sending oxygen-enriched liquid from the column to be vaporized in the top condenser of one of the first columns, and a vaporized oxygen-enriched liquid, A conduit for removing as one oxygen-enriched gas and nitrogen enriched from the first column. Pressurized purified air by cryogenic distillation of air, characterized in that it comprises a conduit for removing the purified fluid and a conduit for removing at least one liquid product from the distillation column system And equipment for the production of liquid products. 第２の蒸留カラム（Ｂ）と、
第２の蒸留カラムに酸素が豊富にされた液体を前記第１のカラムまたは前記塔頂コンデンサから、または、第１のカラムと上記塔頂コンデンサとから供給するための手段と
を具備する
ことを特徴とする請求項１に記載の装置。 A second distillation column (B);
Means for supplying a liquid enriched in oxygen to the second distillation column from the first column or the overhead condenser, or from the first column and the overhead condenser. The device according to claim 1, wherein 最も少ない１つの（the least one）の液体生成物は、液体窒素と液体酸素との内の少なくとも一方を備える
ことを特徴とする請求項１また２に記載の装置。 The apparatus according to claim 1 or 2, wherein the least one liquid product comprises at least one of liquid nitrogen and liquid oxygen.
JP2012006542U 2011-10-28 2012-10-26 Equipment for the production of pressurized purified air and liquid products by cryogenic distillation Expired - Lifetime JP3180832U (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP11306399.4 2011-10-28
EP11306399 2011-10-28

Publications (1)

Publication Number Publication Date
JP3180832U true JP3180832U (en) 2013-01-10

Family

ID=48602663

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2012006542U Expired - Lifetime JP3180832U (en) 2011-10-28 2012-10-26 Equipment for the production of pressurized purified air and liquid products by cryogenic distillation

Country Status (3)

Country Link
JP (1) JP3180832U (en)
KR (1) KR20130002811U (en)
CN (1) CN203011074U (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017078532A (en) * 2015-10-20 2017-04-27 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Oxygen producing system and oxygen producing method
JP6351895B1 (en) * 2018-03-20 2018-07-04 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Nitrogen production method and nitrogen production apparatus
JP2018204825A (en) * 2017-05-31 2018-12-27 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Gas production system

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108079608A (en) * 2017-12-22 2018-05-29 天津科创复兴科技咨询有限公司 A kind of efficient distilation equipment for thering is nitrogen to protect
CN114174747B (en) * 2019-07-26 2024-05-28 乔治洛德方法研究和开发液化空气有限公司 Method and apparatus for separating air by cryogenic distillation
WO2021180362A1 (en) * 2020-03-10 2021-09-16 Linde Gmbh Cryogenic air separation method and air separation unit
KR102600758B1 (en) 2023-07-03 2023-11-10 (주)오디씨티 Purification system for clean dry air

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017078532A (en) * 2015-10-20 2017-04-27 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Oxygen producing system and oxygen producing method
TWI687633B (en) * 2015-10-20 2020-03-11 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 Oxygen production system and oxygen production method
JP2018204825A (en) * 2017-05-31 2018-12-27 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Gas production system
JP6351895B1 (en) * 2018-03-20 2018-07-04 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Nitrogen production method and nitrogen production apparatus
JP2019163905A (en) * 2018-03-20 2019-09-26 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Nitrogen production method and nitrogen production apparatus

Also Published As

Publication number Publication date
CN203011074U (en) 2013-06-19
KR20130002811U (en) 2013-05-09

Similar Documents

Publication Publication Date Title
JP3180832U (en) Equipment for the production of pressurized purified air and liquid products by cryogenic distillation
US8695377B2 (en) Process and apparatus for the separation of air by cryogenic distillation
JP5259703B2 (en) Method and apparatus for cryogenic separation of methane-rich flow
US6314755B1 (en) Double column system for the low-temperature fractionation of air
JP2735742B2 (en) Cryogenic separation method and apparatus for feed air stream
JPH07270066A (en) Cryogenic rectifying system for manufacturing pressure-elevated nitrogen
US4964901A (en) Low-temperature separation of air using high and low pressure air feedstreams
JPH0875349A (en) Air separation method for obtaining gaseous oxygen product at supply pressure
JPH07260343A (en) Cryogenic rectification system using hybrid product boiler
JP2692700B2 (en) Method and apparatus for cryogenic separation of compressed feed air to produce high pressure oxygen and nitrogen products
WO2008059399A3 (en) Cryogenic air separation process and apparatus
WO2010017968A3 (en) Process and device for cryogenic air fractionation
EP2634517B1 (en) Process and apparatus for the separation of air by cryogenic distillation
JP2011518307A5 (en)
US20090120128A1 (en) Low Temperature Air Fractionation with External Fluid
JPH02230079A (en) Manufacture of oxygen by analysis of air
JP6092804B2 (en) Air liquefaction separation method and apparatus
JP2000356464A (en) Low-temperature vapor-depositing system for separating air
JPH10115486A (en) Low temperature distilling method of raw air to manufacture high pressure nitrogen
JP2000346547A (en) Cryogenic distillation for separating air
JPH04227460A (en) Low-temperature nitrogen generator with bottom reboiler and nitrogen expander
JPH07151458A (en) Method and equipment for preparing gaseous oxygen and/or nitrogen under pressure
JP2006329615A (en) Method and device for separating air by low temperature distillation
US8528363B2 (en) Process and apparatus for the separation of air by cryogenic distillation
JP2000356465A (en) Low-temperature distillating system for separating air

Legal Events

Date Code Title Description
R150 Certificate of patent or registration of utility model

Ref document number: 3180832

Country of ref document: JP

Free format text: JAPANESE INTERMEDIATE CODE: R150

Free format text: JAPANESE INTERMEDIATE CODE: R150

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20151212

Year of fee payment: 3

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

EXPY Cancellation because of completion of term