JPH0455682A - Air separating device - Google Patents

Air separating device

Info

Publication number
JPH0455682A
JPH0455682A JP2164686A JP16468690A JPH0455682A JP H0455682 A JPH0455682 A JP H0455682A JP 2164686 A JP2164686 A JP 2164686A JP 16468690 A JP16468690 A JP 16468690A JP H0455682 A JPH0455682 A JP H0455682A
Authority
JP
Japan
Prior art keywords
air
conduit
tank
air separation
heat exchanger
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.)
Pending
Application number
JP2164686A
Other languages
Japanese (ja)
Inventor
Masayuki Tanaka
正幸 田中
Tetsuo Senchi
泉地　哲夫
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kobe Steel Ltd
Original Assignee
Kobe Steel Ltd
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 Kobe Steel Ltd filed Critical Kobe Steel Ltd
Priority to JP2164686A priority Critical patent/JPH0455682A/en
Publication of JPH0455682A publication Critical patent/JPH0455682A/en
Pending legal-status Critical Current

Links

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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • 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
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • F25J3/04333—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
    • F25J3/04351—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 nitrogen
    • 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
    • F25J3/04351—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 nitrogen
    • F25J3/04357—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 nitrogen and comprising a gas work expansion loop
    • 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
    • F25J3/04406—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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • 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
    • F25J2250/42—One fluid being nitrogen
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

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

PURPOSE:To reduce the power consumption for generating cold heat by a method wherein the cold heat energy of liquid constituents of composition, taken out of the tank of the constituents of composition upon supplying product gas, is utilized for the liquefying of N2 taken out of a fractionating tower under the condition of gas. CONSTITUTION:An air separating means A is constituted of an air compressor 11, a main heat exchanger 2 for cooling material air, a fractionating tower 3 for separating LN2 and LO2 from the material air and an expansion turbine 6 for generating cold heat. In a supplying means B, LO2 is sent into an evaporator (second heat exchanger) 7 in accordance with demand from a demanding party by the operation of a pump 51. In this case, heat exchange is effected between the LO2 and GN2 from a conduit 120. According to the heat exchange, the LO2 is gasified and is supplied as product GO2 while GN2 is cooled and liquefied by the LO2 and is reserved in a LN2 tank. The given flow rate of LN2 in the LN2 tank 8 is supplied to the top of the lower tower 31 of the fractionating tower 3 of the air separating means A operated continuously.

Description

【発明の詳細な説明】 〔産業上の利用分野〕 この発明は、原料空気から液体酸素（Ｌｏ２）や液体窒
素（ＬＮ２）などを分離回収し、これらを製鉄所などの
需要先に供給する空気分離装置に関するものである。[Detailed Description of the Invention] [Field of Industrial Application] This invention is an air system that separates and recovers liquid oxygen (Lo2), liquid nitrogen (LN2), etc. from raw air and supplies these to customers such as steel plants. This relates to a separation device.

〔従来の技術〕[Conventional technology]

従来、空気分離手段としては例えば第５図に示すような
ものが知られている。この装置によるプロセスを以下に
説明する。Conventionally, as an air separation means, one shown in FIG. 5, for example, is known. The process using this device will be explained below.

まず原料空気は、原料空気圧縮機１１により圧縮され、
図示しない吸着塔により原料空気中の水分（Ｎ２０）お
よび炭酸ガス（ＣＯ２）などが吸着除去され、前処理さ
れた残りの原料空気が深冷部Ｃ内の主熱交換器２に送ら
れる。この主熱交換器２で上記原料空気は、その沸点近
くまで冷却された後に、導管１１１を通して精溜塔３に
入れられる。First, the raw air is compressed by the raw air compressor 11,
Moisture (N20), carbon dioxide (CO2), and the like in the feed air are adsorbed and removed by an adsorption tower (not shown), and the remaining pretreated feed air is sent to the main heat exchanger 2 in the cryogenic section C. The feed air is cooled to near its boiling point in the main heat exchanger 2 and then introduced into the rectification column 3 through a conduit 111.

この精溜塔３は下塔３１と、上塔３２と、これら両者間
で熱交換を行う主蒸発器３３とから構成され、上記主熱
交換器２からの原料空気はまずこの精溜塔３の下塔３１
下部に入れられる。This rectifying column 3 is composed of a lower column 31, an upper column 32, and a main evaporator 33 that exchanges heat between the two.The raw air from the main heat exchanger 2 is first transferred to the rectifying column lower tower 31
It can be placed at the bottom.

下塔３１に入った原料空気はこの下塔３１内を上昇する
間に還流しＮ２と接触し、しだいにそのＮ２濃度が高め
られ、下塔３１頂部では高純度Ｎ２となる。二〇Ｎ２は
主蒸発器３３に入り上塔３２のＬｏ２と熱交換して凝縮
することによりＬＮ２となる。このＬＮ２は、その一部
が還流液として上塔３２頂部に導管３１１を通して供給
され、残部が還流液として下塔３１頂部に戻される。The raw material air that has entered the lower column 31 comes into contact with reflux and N2 while rising in the lower column 31, and its N2 concentration is gradually increased, and at the top of the lower column 31, it becomes highly purified N2. 20N2 enters the main evaporator 33, exchanges heat with Lo2 in the upper tower 32, and condenses to become LN2. A portion of this LN2 is supplied as a reflux liquid to the top of the upper column 32 through the conduit 311, and the remainder is returned to the top of the lower column 31 as a reflux liquid.

この還流液は下塔３１を下っていく間にこの下塔３１内
を上昇してくる原料空気と接触して０２濃度が高められ
、この下塔３１底部に０２が４０％程度含まれる液体空
気となって溜められる。そしてこの液体空気は下塔３１
底部から取出されて上塔３２中部に導管３１２を通して
供給される。While going down the lower column 31, this reflux liquid comes into contact with the raw material air rising in the lower column 31, and the 02 concentration is increased, and the liquid air containing about 40% 02 at the bottom of the lower column 31. It is accumulated as follows. And this liquid air is in the lower tower 31
It is taken out from the bottom and fed into the middle of the upper column 32 through a conduit 312.

この液体空気は、上塔３２中部から下方に流れる間に０
２が濃縮されて上塔３２底部には高純度のＬＯ２が溜り
、このＬＯ２は上記蒸発器３３のＮ２と熱交換してガス
化した後、導管３２０を通してガス酸素（以下ＧＯ２と
いう）として取出される。このＣＯ２は主熱交換器２に
上記導管３２０を通して送られ、この主熱交換器２で原
料空気と熱交換され、これが製品ＧＯ２として需要先に
供給される。一方、上塔３２頂部からは高純度Ｎ２が取
出され、この高純度Ｎ２は主熱交換器２に導管３２１を
通して送られ、この主熱交換器２で原料空気を冷却した
後、製品ガス窒素（以下製品ＧＮ２という）として需要
先に供給される。While this liquid air flows downward from the middle of the upper tower 32, it becomes zero.
2 is concentrated and high-purity LO2 accumulates at the bottom of the upper column 32, and this LO2 is gasified by heat exchange with N2 in the evaporator 33, and then taken out as gaseous oxygen (hereinafter referred to as GO2) through the conduit 320. Ru. This CO2 is sent to the main heat exchanger 2 through the conduit 320, where it exchanges heat with the raw material air, and is supplied to customers as product GO2. On the other hand, high-purity N2 is taken out from the top of the upper column 32, and this high-purity N2 is sent to the main heat exchanger 2 through a conduit 321. After cooling the feed air in the main heat exchanger 2, the product gas nitrogen ( The product is supplied to demand customers as product GN2 (hereinafter referred to as product GN2).

また上記しＮ２、Ｌ○２の分離精製のための寒冷は、膨
張タービン６によって原料空気の一部を断熱膨張させて
発生させ、これを精溜塔３の上塔３２中部に導管６００
を通して供給している。Furthermore, the above-mentioned refrigeration for separating and refining N2 and L○2 is generated by adiabatically expanding a part of the raw material air using the expansion turbine 6, and this is sent to the middle part of the upper column 32 of the rectification column 3 through a conduit 600.
It is supplied through.

なお上塔３２上部からは純度の低いＮ２が図示しない導
管を通して取出され、この低純度Ｎ２を利用して上記前
処理用吸着塔の再生が行われる。Note that low-purity N2 is taken out from the upper part of the upper column 32 through a conduit (not shown), and this low-purity N2 is used to regenerate the pretreatment adsorption column.

一方、上記需要先が転炉や電気炉などを用いた製鉄所で
ある場合には、上記製品ＧＯ２などの消費特性が連続的
でなく、間欠的であるために、上記空気分離手段からの
製品ＧＯ２などの供給も間欠的に行う必要がある。とこ
ろが、上記空気分離手段においては、定常状態での運転
を継続することによりほぼ一定の純度の製品ＧＮ２や製
品Ｇ０２が効率良く得られるために、需要先での需要に
応じてその運転を途中で急に停止したり変動させたりす
ることはできない。On the other hand, if the above-mentioned demand destination is a steel mill using a converter or an electric furnace, the consumption characteristics of the above-mentioned product GO2 etc. are not continuous but intermittent, so the product from the above-mentioned air separation means is It is also necessary to supply GO2 and the like intermittently. However, in the above-mentioned air separation means, products GN2 and G02 of almost constant purity can be efficiently obtained by continuing operation in a steady state, so the operation may be stopped midway depending on the demand at the customer. It cannot be suddenly stopped or changed.

このため従来は、第５図に示す空気分離手段と需要先と
の間に製品Ｇｏ２などを蓄えるガスホルダーＨからなる
供給手段を設けることが行なわれている。この場合は、
上記空気分離手段の連続運転により製造された製品Ｇｏ
２などを上記ガスホルダーに高圧下で蓄え、このガスホ
ルダーＨから製品ＧＯ２などを需要に応じて需要先へ供
給するようにされる。For this reason, conventionally, a supply means consisting of a gas holder H for storing the product Go2 and the like has been provided between the air separation means shown in FIG. 5 and the consumer. in this case,
Product Go manufactured by continuous operation of the above air separation means
2 and the like are stored under high pressure in the gas holder H, and the product GO2 and the like are supplied from this gas holder H to the demand destination according to demand.

〔発明が解決しようとする課題〕[Problem to be solved by the invention]

ところが、供給手段として上記ガスホルダーＨを設けた
場合には、需要先への供給が停止されている間も製品Ｇ
Ｏ２などがガスホルダーに蓄えられるために、比較的大
容量のガスホルダーが必要となる。このためこのガスホ
ルダーによって空気分離装置がかなり大規模になる。However, if the gas holder H is installed as a supply means, the product
Since O2 and the like are stored in the gas holder, a relatively large capacity gas holder is required. This gas holder therefore makes the air separation device quite large.

ここで空気分離装置をコンパクトにするために、第６図
に示すように供給手段として製品ＬＮ２タンク４や製品
Ｌ０２タンク５を設け、これらのタンクにＮ２や０２を
ガスの状態ではなく液体の状態で蓄えるようにすること
が考えられる。この場合には、精溜塔３の下塔３１頂部
のＬＮ２が導管３１１を通して取出される際に、そのＬ
Ｎ２の一部が製品ＬＮ２として導管４００を通して上記
製品ＬＮ２タンク４に取出され、また精溜塔３の上塔３
２底部のＬＯ２が導管５００を通して製品ＬＯ２として
製品ＬＯ。タンク５に取出される。そしてこの製品ＬＮ
２タンク４や製品ＬＯ２タンク５からは、ＬＮ２やＬＯ
２が需要先からの需要に応じてポンプ４１．５１によっ
て取出され、このＬＮ２やＬ０２は蒸発器４０．５０に
よってガス化され、製品ＧＮ２や製品Ｇｏ２として需要
先に供給される。In order to make the air separation device more compact, a product LN2 tank 4 and a product L02 tank 5 are provided as supply means as shown in FIG. One idea is to store it in In this case, when the LN2 at the top of the lower column 31 of the rectification column 3 is taken out through the conduit 311, the LN2
A part of the N2 is taken out as product LN2 through the conduit 400 to the product LN2 tank 4, and also to the upper column 3 of the rectification column 3.
2 bottom LO2 passes through conduit 500 to product LO2 as product LO2. It is taken out to tank 5. And this product LN
2 tank 4 and product LO2 tank 5, LN2 and LO
2 is taken out by a pump 41.51 in response to demand from a consumer, and this LN2 and L02 are gasified by an evaporator 40.50 and supplied to the consumer as product GN2 and product Go2.

ところが第６図に示す供給手段と空気分離手段とを組合
せた構成では、蒸発器４０．５０において製品ＬＮ２や
製品ＬＯ２が大気や温水などと熱交換されるために、こ
の製品ＬＮ２や製品ＬＯ２が有する冷熱エネルギーがま
ったく利用されないまま無駄に放出されてしまう。However, in the configuration in which the supply means and the air separation means are combined as shown in FIG. The available cooling energy is not utilized at all and is wasted.

この発明は、このような事情に鑑みてなされたものであ
り、需要先での需要変動に対応して製品ガスを供給する
ことができ、しかも供給に際するエネルギーを有効利用
して液化分離に伴う動力消費を低減することができる空
気分離装置を提供することを目的としている。This invention was made in view of the above circumstances, and it is possible to supply product gas in response to demand fluctuations at the customer, and moreover, it is possible to effectively utilize the energy during supply to perform liquefaction separation. It is an object of the present invention to provide an air separation device that can reduce the accompanying power consumption.

〔課題を解決するための手段〕[Means to solve the problem]

上記目的を達成するために、この発明の請求項１では、
空気圧縮機と、この空気圧縮機により取入れた原料空気
を冷却する主熱交換器と、冷却された原料空気から選択
的に組成成分を液状で分離する精溜塔とを有する空気分
離手段からなる空気分離装置において、上記空気分離手
段には上記液状組成成分を気化させて需要先に供給する
供給手段が設けられ、この供給手段は上記液状組成成分
を蓄えるように上記精溜塔と接続された組成成分タンク
と、上記精留塔での分離過程で生成されたＮ２を上記組
成成分タンクから取出した液状組成成分によって冷却す
る第２の熱交換器と、この第２の熱交換器によって液化
されたＮ２を蓄えるＬＮ２タンクとが備えられ、このＬ
Ｎ２タンクと精溜塔とは上記しＮ２タンク内のＬＮ２を
精溜塔に供給可能に互いに接続されているように構成し
た。In order to achieve the above object, in claim 1 of this invention,
Consisting of an air compressor, a main heat exchanger that cools the feed air taken in by the air compressor, and a rectification column that selectively separates constituent components in liquid form from the cooled feed air. In the air separation device, the air separation means is provided with a supply means for vaporizing the liquid composition component and supplying it to a consumer, and this supply means is connected to the rectification column so as to store the liquid composition component. a component tank; a second heat exchanger that cools N2 generated in the separation process in the rectification column with the liquid component taken out from the component tank; This LN2 tank is equipped with an LN2 tank that stores N2.
The N2 tank and the rectification column were configured to be connected to each other so that the LN2 in the N2 tank could be supplied to the rectification column as described above.

請求項２では、請求項１において複数の空気分離手段と
、一つの供給手段とによって構成されるようにした。In a second aspect of the present invention, the air conditioner according to the first aspect is constituted by a plurality of air separation means and one supply means.

請求項３では、液状組成成分がＬ０２であるように構成
した。In claim 3, the liquid composition component is L02.

請求項４では、ＬＮ２タンクからのＬＮ２が精溜塔に分
離のためなどの寒冷源として供給されるように構成した
。In claim 4, the LN2 tank is configured to supply LN2 from the LN2 tank to the rectification column as a cold source for separation.

請求項５では、空気分離手段と供給手段とで必要なすべ
ての寒冷を発生する寒冷発生手段を上記供給手段側に設
けて構成した。In a fifth aspect of the present invention, a cold generation means for generating all the cold necessary for the air separation means and the supply means is provided on the side of the supply means.

〔作用〕[Effect]

上記請求項１の構成によれば、組成成分タンクから取出
された液状組成成分の冷熱エネルギーによって、精留塔
からガス状態で取出されたＮ２が液化されるために、上
記冷熱エネルギーを有効利用することができる。さらに
液化されたＮ２を還流ＬＮ２および寒冷源として精溜塔
に送ることにより、寒冷発生のための動力を低減するこ
とができる。According to the configuration of claim 1, the N2 taken out in a gaseous state from the rectification column is liquefied by the cold energy of the liquid composition taken out from the composition tank, so that the cold energy is effectively used. be able to. Further, by sending the liquefied N2 to the rectification column as the reflux LN2 and a cold source, the power required for generating cold can be reduced.

請求項２の構成によれば、一つの空気分離手段に対して
一つの供給手段を組合せる場合と比べて装置がコンパク
トになる。According to the structure of claim 2, the apparatus becomes more compact than when one supply means is combined with one air separation means.

〔実施例〕〔Example〕

第１実施例を示す第１図において、空気分離装置は空気
分離手段Ａと供給手段Ｂとから構成される。空気分離手
段Ａは、空気圧縮機１１と、原料空気を前処理する吸着
塔（図示せず）と、原料空気を冷却する主熱交換器２と
、原料空気からＬＮ２およびＬ０２を分離する精溜塔３
と、寒冷を発生させる膨張タービン６とから基本構成さ
れている。また供給手段Ｂは、製品ＬＯ２を蓄える製品
Ｌ０２タンク５と、このタンク５から製品Ｌｏ２を取出
すポンプ５１と、Ｎ２圧縮機１２と、上記製品ＬＯ２と
このＮ２圧縮機１２によって送られてくるＮ２とを互い
に熱交換させる蒸発器（第２の熱交換器）７と、この蒸
発器７によって液化されたＮ２を蓄える（Ｎ２タンク８
とから基本構成されている。In FIG. 1 showing the first embodiment, the air separation apparatus is composed of air separation means A and supply means B. In FIG. The air separation means A includes an air compressor 11, an adsorption tower (not shown) that pre-treats the feed air, a main heat exchanger 2 that cools the feed air, and a rectifier that separates LN2 and L02 from the feed air. tower 3
It basically consists of: and an expansion turbine 6 that generates cold. In addition, the supply means B includes a product L02 tank 5 for storing the product L02, a pump 51 for taking out the product L02 from the tank 5, an N2 compressor 12, and the product L02 and the N2 sent by the N2 compressor 12. An evaporator (second heat exchanger) 7 that exchanges heat with each other, and an N2 tank 8 that stores N2 liquefied by this evaporator 7.
It basically consists of.

上記空気分離手段Ａにおける前処理用吸着塔は一対の吸
着器からなり、一方の吸着器で原料空気から水分（Ｎ２
０）および炭酸ガス（ＣＯ２）を吸着除去する間に、他
方の吸着器は精溜塔３からの比較的低純度のＮ２によっ
て再生されるように構成されている。The adsorption tower for pretreatment in the air separation means A is composed of a pair of adsorbers, one of which is used to extract moisture (N2
0) and carbon dioxide (CO2), the other adsorber is configured to be regenerated by relatively low purity N2 from the rectification column 3.

上記空気圧縮機１１は上記前処理用吸着塔が介在された
導管１１０によって主熱交換器２と接続され、この主熱
交換器２は導管１１１によって精溜塔３の下塔３１下部
と接続される。主熱交換器２でその液化温度付近まで冷
却された原料空気は、導管１１１によって下塔３１下部
に導入される。The air compressor 11 is connected to the main heat exchanger 2 through a conduit 110 in which the pretreatment adsorption tower is interposed, and the main heat exchanger 2 is connected to the lower part of the lower column 31 of the rectification column 3 through a conduit 111. Ru. The raw air cooled to around its liquefaction temperature in the main heat exchanger 2 is introduced into the lower part of the lower column 31 through a conduit 111.

上記精溜塔３は、下塔３１と、上塔３２と、これらの間
に設けられた蒸発器３３とから構成される。下塔３１頂
部には受皿３４が設けられ、この受皿３４には導管３１
１の一端が接続され、その他端は上塔３２上部に接続さ
れている。下塔３１底部には導管３１２の一端が接続さ
れ、この導管３１２の他端は上塔３２中部と接続されて
いる。The rectifying column 3 is composed of a lower column 31, an upper column 32, and an evaporator 33 provided between them. A saucer 34 is provided at the top of the lower tower 31, and the conduit 31 is placed in the saucer 34.
1 is connected, and the other end is connected to the upper part of the upper tower 32. One end of a conduit 312 is connected to the bottom of the lower tower 31, and the other end of this conduit 312 is connected to the middle part of the upper tower 32.

また上記上塔３２頂部には導管３２１の一端が接続され
、この導管３２１の他端は主熱交換器２と接続されてい
る。この主熱交換器２には、導管３２２の一端か上記導
管３２１と互いに連通するように接続され、その他端は
供給手段ＢのＮ２圧縮機１２と接続されている。また上
塔３２底部には導管５００の一端が接続され、この導管
５００の他端はＬ０２タンク５と接続されている。Further, one end of a conduit 321 is connected to the top of the upper tower 32, and the other end of this conduit 321 is connected to the main heat exchanger 2. One end of the conduit 322 is connected to the main heat exchanger 2 so as to communicate with the conduit 321, and the other end is connected to the N2 compressor 12 of the supply means B. Further, one end of a conduit 500 is connected to the bottom of the upper tower 32, and the other end of this conduit 500 is connected to the L02 tank 5.

上記導管１１０は主熱交換器２内で分岐され、この分岐
管６００は膨脹タービン６を介して精溜塔３の上塔３２
中部に接続されている。さらに上塔３２上部には図示し
ない導管が接続され、この導管は主熱交換器２を介して
再生用ガスを前処理用吸着塔に供給するように上記前処
理用吸着塔と接続されている。The conduit 110 is branched within the main heat exchanger 2, and this branch pipe 600 is connected to the upper column 32 of the rectification column 3 via the expansion turbine 6.
Connected to the central part. Furthermore, a conduit (not shown) is connected to the upper part of the upper column 32, and this conduit is connected to the pretreatment adsorption tower so as to supply regeneration gas to the pretreatment adsorption tower via the main heat exchanger 2. .

ＬＯ２タンク５にはポンプ５１が接続され、このポンプ
５１は導管５１１によってＬＯ３を送給可能に蒸発器７
と接続され、この蒸発器７はガス化された製品Ｇ０２を
転炉や電気炉などを有する製鉄所（需要先）まで送給可
能に導管５１２によって上記需要先と接続されている。A pump 51 is connected to the LO2 tank 5, and this pump 51 can supply LO3 to the evaporator 7 through a conduit 511.
The evaporator 7 is connected to the customer through a conduit 512 so that the gasified product G02 can be delivered to the steelworks (the customer) having a converter, electric furnace, etc.

またＮ２圧縮機１２は導管１２０によって蒸発器７と接
続され、この蒸発器７は液化されたＮ２を送給可能に導
管１２１によってＬＮ２タンク８と接続されている。さ
らにこのＬＮ２タンク８には導管１２２の一端が接続さ
れ、この導管１２２の他端はＬＮ２を送給可能に精溜塔
３の下塔３１頂部と接続されている。The N2 compressor 12 is also connected to the evaporator 7 by a conduit 120, and the evaporator 7 is connected to the LN2 tank 8 by a conduit 121 so that liquefied N2 can be delivered. Further, one end of a conduit 122 is connected to this LN2 tank 8, and the other end of this conduit 122 is connected to the top of the lower column 31 of the rectification column 3 so that LN2 can be supplied.

つぎに、上記構成の空気分離装置によるプロセスを、ま
ず空気分離手段Ａでの基本的なプロセスから説明する。Next, the process performed by the air separation apparatus having the above configuration will be explained, starting with the basic process in the air separation means A.

原料空気は、第１の空気圧縮機１１により圧縮され、図
示しない吸着塔により原料空気中の水分（Ｎ２０）およ
び炭酸ガス（ＣＯ２）などが吸着除去され、前処理され
た残りの原料空気が深冷部Ｃ内の主熱交換器２に導管１
１０を通して送られる。この主熱交換器２で上記原料空
気は、その沸点近くまで冷却された後に、導管１１１を
通して精溜塔３の下塔３１に入れられる。The raw air is compressed by the first air compressor 11, moisture (N20), carbon dioxide (CO2), etc. in the raw air are adsorbed and removed by an adsorption tower (not shown), and the remaining pretreated raw air is deep-seated. Conduit 1 to main heat exchanger 2 in cold section C
Sent through 10. The feed air is cooled to near its boiling point in the main heat exchanger 2 and then introduced into the lower column 31 of the rectification column 3 through a conduit 111.

下塔３１に入った原料空気はこの下塔３１内を上昇する
間に還流しＮ２と接触し、しだいにそのＮ２濃度が高め
られ、下塔３１頂部では高純度Ｎ２となる。このＮ２は
主蒸発器３３に入り上塔３２のＬ０２と熱交換して凝縮
することによりＬＮ２となる。このＬＮ２は、その一部
が還流液として上塔３２頂部に導管３１１を通して供給
され、残部が還流液として下塔３１頂部に戻される。The raw material air that has entered the lower column 31 comes into contact with reflux and N2 while rising in the lower column 31, and its N2 concentration is gradually increased, and at the top of the lower column 31, it becomes highly purified N2. This N2 enters the main evaporator 33, exchanges heat with L02 in the upper column 32, and condenses to become LN2. A portion of this LN2 is supplied as a reflux liquid to the top of the upper column 32 through the conduit 311, and the remainder is returned to the top of the lower column 31 as a reflux liquid.

この還流液は下塔３１を下っていく間にこの下塔３１内
を上昇してくる原料空気と接触して０２濃度が高められ
、この下塔３１底部に０゜が４０％程度含まれる液体空
気となって溜められる。そしてこの液体空気は下塔３１
底部から取出されて上塔３２中部に導管３１２を通して
供給される。While this reflux liquid goes down the lower column 31, it comes into contact with the raw material air rising in the lower column 31, and the 02 concentration is increased, and the bottom of the lower column 31 contains a liquid containing about 40% of 0°. It becomes air and accumulates. And this liquid air is in the lower tower 31
It is taken out from the bottom and fed into the middle of the upper column 32 through a conduit 312.

この液体空気は、上塔３２中部から下方に流れる間に０
２が濃縮されて上塔３２底部には高純度のＬＯ２が溜り
、このＬ０２の一部は蒸発器３３でＮ２と熱交換してＬ
ｏ２は蒸発してＣＯ２となり、これが上塔３２での精溜
塔上昇ガスとなって精留操作が行われる。残りのＬＯ２
は導管５００を通して取出され、Ｌ０２タンク５に蓄え
られる。While this liquid air flows downward from the middle of the upper tower 32, it becomes zero.
2 is condensed and high-purity LO2 accumulates at the bottom of the upper column 32, and a part of this L02 is exchanged with N2 in the evaporator 33 to become L02.
The o2 evaporates to become CO2, which becomes the rising gas in the rectification column in the upper column 32 and performs the rectification operation. remaining LO2
is removed through conduit 500 and stored in L02 tank 5.

また空気圧縮機１２によって主熱交換器２に送られた原
料空気の一部は膨脹タービン６で断熱膨脹されて寒冷が
発生され、これが精溜塔３の上塔３２中部に導管６００
を通して供給される。Further, a part of the raw air sent to the main heat exchanger 2 by the air compressor 12 is adiabatically expanded by the expansion turbine 6 to generate cold, which is passed through the conduit 600 to the middle of the upper column 32 of the rectification column 3.
supplied through.

一方、上塔３２頂部からは高純度Ｎ２が取出され、この
高純度Ｎ２は主熱交換器２に導管３２１を通して送られ
、この主熱交換器２で原料空気を冷却する。この主熱交
換器２で原料空気と熱交換したＧＮ２は、導管３２２を
通して供給手段ＢのＮ２圧縮機１２に送られ、このＮ２
圧縮機１２で圧縮されて導管１２０を通して蒸発器７に
送られる。On the other hand, high-purity N2 is taken out from the top of the upper column 32, and is sent to the main heat exchanger 2 through a conduit 321, where the feed air is cooled. The GN2 that has undergone heat exchange with the raw air in the main heat exchanger 2 is sent to the N2 compressor 12 of the supply means B through the conduit 322, and this N2
It is compressed by compressor 12 and sent to evaporator 7 through conduit 120.

また上記供給手段Ｂでは、ポンプ５１の作動により需要
先からの需要に応じてＬ０２が蒸発器７に導管５１１を
通して送られる。この蒸発器７では上記しＯ２と、上記
導管１２０からのＧＮ２とが熱交換される。これによっ
て上記しＯ２はガス化され、製品Ｇ０２として導管５１
２を通して需要先に供給されるとともに、上記ＧＮ２は
上記Ｌ０２によって冷却されて液化し、ＬＮ２が導管１
２１を通してＬＮ２タンク８に蓄えられる。このＬＮ２
タンク８のＬＮ２は、連続運転されている空気分離手段
Ａの精溜塔３へ導管１２２を通してその下塔３１頂部に
一定流量供給される。これによって上記ＬＮ２は精留塔
３内での還流しＮ２として利用されるとともに、分離に
際する寒冷源の一部としても利用される。Further, in the supply means B, L02 is sent to the evaporator 7 through the conduit 511 according to the demand from the consumer by operating the pump 51. In this evaporator 7, the above-described O2 and the GN2 from the conduit 120 are heat exchanged. As a result, the O2 mentioned above is gasified, and the product G02 is produced in the conduit 51.
At the same time, the GN2 is cooled and liquefied by the L02, and LN2 is supplied to the consumer through the conduit 1.
21 and is stored in the LN2 tank 8. This LN2
LN2 in the tank 8 is supplied at a constant flow rate to the top of the lower column 31 of the rectification column 3 of the air separation means A, which is continuously operated, through the conduit 122. As a result, the LN2 is used as refluxed N2 in the rectification column 3, and is also used as part of the cold source during separation.

このように導管６００を通して供給される膨張タービン
６からの寒冷の他に、導管１２２を通して供給手段Ｂか
らＬＮ２としての寒冷が精溜塔３に供給されるために、
このＬＮ２が供給されない場合と比べて、空気分離手段
Ａでの寒冷発生量を上記供給手段Ｂから供給される寒冷
の分だけ減らすことができ、これによりその寒冷発生に
要する動力を低減することができる。In addition to the refrigeration from the expansion turbine 6 supplied through the conduit 600, refrigeration as LN2 is supplied to the rectification column 3 from the supply means B through the conduit 122.
Compared to the case where this LN2 is not supplied, the amount of cold generated by the air separation means A can be reduced by the amount of cold supplied from the supply means B, thereby reducing the power required to generate the cold. can.

さらに従来の供給手段としてガスホルダーＨ（第５図参
照）を用いる場合に比べて、需要先に供給する製品を液
体の状態で蓄えることができるために、装置全体をコン
パクトにすることができる。Furthermore, compared to the case where a gas holder H (see FIG. 5) is used as a conventional supply means, the product to be supplied to a customer can be stored in a liquid state, so that the entire apparatus can be made more compact.

第２図には第２実施例が示されている。これは、第１実
施例（第１図参照）の構成に導管３２３および３２４を
付加するとともに、上記第１実施例における導管３２２
にＧＮ２取出し用分岐管３２２ａ、１２０ａを設けたも
のである。上記導管３２３は、その一端が精留塔３の上
塔３２の底部、他端が主熱交換器２にそれぞれ接続され
、上記導管３２４はその一端が上記導管３２３と互いに
連通するように上記主熱交換器２に接続され、上記導管
３２４の他端は導管５１２と合流するように接続されて
いる。すなわち上記導管３２３によって上塔３２から取
出されたＧＯ２は主熱交換器２に送られ、主熱交換器２
で原料空気を冷却することにより熱交換され、この熱交
換後の６０２が導管３２４を通して導管５１２内のＧＯ
２と合流される。A second embodiment is shown in FIG. This adds conduits 323 and 324 to the configuration of the first embodiment (see FIG. 1), and also adds conduits 323 and 324 to the configuration of the first embodiment (see FIG. 1).
Branch pipes 322a and 120a for taking out GN2 are provided in the main body. The conduit 323 has one end connected to the bottom of the upper column 32 of the rectification column 3, and the other end connected to the main heat exchanger 2, and the conduit 324 has one end connected to the main heat exchanger 2 so as to communicate with the conduit 323. The conduit 324 is connected to the heat exchanger 2, and the other end of the conduit 324 is connected to join the conduit 512. That is, GO2 taken out from the upper tower 32 through the conduit 323 is sent to the main heat exchanger 2;
The raw air is cooled at
It will be merged with 2.

また導管３２２の途中には分岐管３２２ａが上記導管３
２２内のＧＮ２を取出し可能に設けられ、また導管１２
０の途中には分岐管１２０ａが上記導管１２０内のＧＮ
２を取出し可能に設けられている。Further, a branch pipe 322a is provided in the middle of the conduit 322.
GN2 in the conduit 12 can be taken out.
0, a branch pipe 120a is connected to the GN in the conduit 120.
2 can be taken out.

この第２実施例によれば、需要先へ供給可能な製品Ｇ０
２の供給源として導管５１２からのものと、導管３２４
からのものとの２経路を設けることができる。この導管
３２４からのＧＯ２は空気分離手段Ａの定常運転により
一定流量が継続して供給されるために、この導管３２４
からのＧＯ２を需要先で最低限必要とする一定供給量（
ベースロード量）と対応させて供給するようにし、そし
て需要量の変動時、すなわち上記一定供給量を超える一
時的な需要増に対してはＬＯ２タンク５から蒸発させた
導管５１２からの６０２により対処するようにすること
ができる。したがって需要先の様々な需要変動に対して
も、空気分離手段Ａの定常運転を維持しつつ、より確実
に対処することができる。According to this second embodiment, the product G0 that can be supplied to the demand destination
2 from conduit 512 and from conduit 324.
It is possible to provide two routes to and from. Since GO2 from this conduit 324 is continuously supplied at a constant flow rate due to the steady operation of the air separation means A, this conduit 324
The minimum required supply amount of GO2 from the demand destination (
602 from the conduit 512 evaporated from the LO2 tank 5 is used to deal with fluctuations in demand, that is, temporary increases in demand exceeding the above-mentioned constant supply amount. You can do as you like. Therefore, it is possible to more reliably cope with various demand fluctuations at the demand destination while maintaining steady operation of the air separation means A.

また上記第２実施例によれば、分岐管３２２ａを通して
低圧の製品ＧＮ２、分岐管１２０ａを通してＮ２圧縮機
１２により圧縮された高圧の製品ＧＮ２をそれぞれ取出
すことができる。これにより需要先での要求に応じて低
圧もしくは高圧の製品ＧＮ２の供給を行うことができる
。しかも、この第２実施例では、一つのＮ２圧縮機１２
によりＧＮ２の圧送のための加圧と、製品として要求さ
れる所定圧力への加圧との両機能を発揮させることがで
き、装置全体のコンパクト化に寄与することができる。Further, according to the second embodiment, the low-pressure product GN2 can be taken out through the branch pipe 322a, and the high-pressure product GN2 compressed by the N2 compressor 12 can be taken out through the branch pipe 120a. This makes it possible to supply the low-pressure or high-pressure product GN2 according to the demands of the demand destination. Moreover, in this second embodiment, one N2 compressor 12
This makes it possible to perform both functions of pressurizing the GN2 and pressurizing to a predetermined pressure required as a product, thereby contributing to making the entire device more compact.

第３図には第３実施例が示されている。これは上記第２
実施例（第２図参照）の構成に新たに他の蒸発器９など
を付加したものである。この第３実施例では、ＬＮ２タ
ンク８に導管８００の一端が接続され、この導管８００
の他端が上記蒸発器９と接続され、この導管８００を通
して上記ＬＮ２タンク８内のＬＮ２が上記蒸発器９に供
給される。そしてこの蒸発器９の出口側には導管８１０
の一端が接続され、この導管８１０を通して上記蒸発器
９てガス化したＮ２　　（ＧＮ２　）が大気に放出され
る。A third embodiment is shown in FIG. This is the second above
This is a configuration in which another evaporator 9 and the like are newly added to the configuration of the embodiment (see FIG. 2). In this third embodiment, one end of a conduit 800 is connected to the LN2 tank 8, and this conduit 800
The other end is connected to the evaporator 9, and LN2 in the LN2 tank 8 is supplied to the evaporator 9 through this conduit 800. A conduit 810 is provided on the outlet side of this evaporator 9.
N2 (GN2) gasified in the evaporator 9 is discharged to the atmosphere through this conduit 810.

また導管３２４と合流した後、需要先までのばされた導
管５１２には、製品Ｇ０２を需要先まで圧送するための
０２圧縮機１３が介在されるとともに、この０２圧縮機
１３の下流側に製品ＧＯ２を引込み可能に分岐管５１３
の一端が接続されている。この分岐管５１３の他端は上
記蒸発器９に接続され、上記分岐管５１３を通して送ら
れた製品Ｇ○２が上記蒸発器９で導管８００からのＬＮ
２によって冷却、液化される。この蒸発器９とＬ○２タ
ンク５とは導管５１４によって接続され、この導管５１
４を通して上記蒸発器９で液化された０２（ＬＯ２）が
上記Ｌ０２タンク５に戻される。In addition, in the conduit 512 that is extended to the demand destination after merging with the conduit 324, an 02 compressor 13 is interposed to convey the product G02 under pressure to the demand destination. Branch pipe 513 that allows GO2 to be drawn in
is connected at one end. The other end of this branch pipe 513 is connected to the evaporator 9, and the product G○2 sent through the branch pipe 513 is transferred to the evaporator 9 from LN from the conduit 800.
2, it is cooled and liquefied. This evaporator 9 and L○2 tank 5 are connected by a conduit 514, and this conduit 51
4, the 02 (LO2) liquefied in the evaporator 9 is returned to the L02 tank 5.

この第３実施例では、０゜圧縮機１３によって圧縮され
、導管５１２を通して需要先に供給される途中において
も、その導管５１２内の製品Ｇ０２を分岐管５１３によ
って蒸発器９に導き、この蒸発器９で液化することによ
り、Ｌ０２タンク５に戻すことができる。これにより需
要先での急激な需要変動、例えば需要量がピーク値から
急減した場合などに、その変動が大きすぎたり、早すぎ
たりして上記０２圧縮機１３が上記変動に追従できない
ときに、上記分岐管５１３から製品Ｇ○２を分岐させる
ことにより、上記変動に対１．でも対処することができ
る。しかも分岐させた製品Ｇ。In this third embodiment, the product G02 in the conduit 512 is guided to the evaporator 9 through the branch pipe 513 even while being compressed by the 0° compressor 13 and being supplied to the consumer through the conduit 512. By liquefying it in step 9, it can be returned to the L02 tank 5. As a result, when there is a sudden change in demand at a demand destination, such as when the demand quantity suddenly decreases from its peak value, the 02 compressor 13 cannot follow the change because the change is too large or too fast. By branching the product G○2 from the branch pipe 513, the above fluctuation can be addressed in 1. But it can be dealt with. Moreover, it is a branched product G.

２を廃棄することなく、ＬＯ２に変換させてＬＯ２タン
ク５に再び戻すことができ、ロスを無くすことができる
。さらに上記製品ＧＯ２をＬ０２に液化するエネルギー
として、特別な冷熱を使用せずに空気分離手段Ａの運転
により大量に得られたＬＮ２タンク８内のＬＮ２を用い
ているために、効率的に行うことができる。2 can be converted into LO2 and returned to the LO2 tank 5 without being discarded, thereby eliminating loss. Furthermore, as the energy for liquefying the product GO2 into L02, the LN2 in the LN2 tank 8 obtained in large quantities by the operation of the air separation means A is used without using special cold energy, so it can be done efficiently. I can do it.

第４図には第４実施例が示されている。これは供給手段
Ｂ側に設けた膨脹タービン６ａによって第１実施例（第
１図参照）における空気分離手段Ａの膨脹タービンを省
略するように構成したものである。すなわち供給手段Ｂ
の蒸発器７に膨脹タービン（寒冷発生手段）６ａを設け
、この膨脹タービンによってＮ２圧縮機１２からのＮ２
の一部を断熱膨張させて寒冷を発生させ、この寒冷によ
って蒸発器７でのＮ２の液化を促進し、ここで得られる
寒冷をＬＮ２の形で空気分離手段Ａに与えるように構成
したものである。これにより、空気分離手段Ａで分離な
どに必要な寒冷や供給手段Ｂでの低温維持のための寒冷
などが上言己膨張タービン６ａによって発生され、これ
により第１実施例における空気分離手段Ａでの膨脹ター
ビン６（第１図参照）を省略することができ、上記空気
分離手段Ａのコンパクト化を図ることができる。A fourth embodiment is shown in FIG. This configuration is such that the expansion turbine 6a provided on the supplying means B side is used to omit the expansion turbine of the air separation means A in the first embodiment (see FIG. 1). That is, supply means B
An expansion turbine (cold generation means) 6a is provided in the evaporator 7 of the evaporator 7, and the N2 from the N2 compressor 12 is
A portion of the LN2 is adiabatically expanded to generate cold, this cold promotes the liquefaction of N2 in the evaporator 7, and the cold obtained here is supplied to the air separation means A in the form of LN2. be. As a result, the self-expansion turbine 6a generates the cold necessary for separation in the air separation means A and the cold for maintaining low temperature in the supply means B, and thereby the air separation means A in the first embodiment The expansion turbine 6 (see FIG. 1) can be omitted, and the air separation means A can be made more compact.

なお上記第１〜第４の実施例における他の態様を以下に
説明する。Other aspects of the first to fourth embodiments will be described below.

Ａ、上記実施例では、一つの空気分離手段Ａと一つの供
給手段Ｂとによって空気分離装置を構成しているが、こ
れに限らず、複数の空気分離装置Ａ、Ａ、・・・と一つ
の供給手段Ｂとによって空気分離装置を構成してもよい
。この場合には複数の精溜塔からのＬ０２を一つのＬＯ
２タンクに蓄えるとともに、一つのＬＮ２タンクから複
数の精溜塔にＬＮ２が供給されるように構成すればよい
。これによつて一つの空気分離手段Ａ毎に一つの供給手
段Ｂを備える場合に比べて装置がコンパクトになる。A. In the above embodiment, the air separation device is composed of one air separation means A and one supply means B, but it is not limited to this. The air separation device may be constituted by two supply means B. In this case, L02 from multiple rectification columns is combined into one LO
LN2 may be stored in two tanks and may be configured to be supplied from one LN2 tank to a plurality of rectification columns. This makes the apparatus more compact than when one supply means B is provided for each air separation means A.

Ｂ、上記実施例では、精留塔から取出す液状組成成分と
してＬ０２を選択し、原料空気からＧＮ２とＬＯ２とを
分離してそのＬＯ２から得られるＧＯ２を需要先に供給
するようにしているが、これに限らず、上記しＯ２に加
えて、例えば精留塔の受皿３４からＬＮ２を液状組成成
分として取出して製品として需要先に供給するように構
成してもよい。さらに原料空気からアルゴンを液状で分
離して需要先に供給するように構成してもよい。B. In the above example, L02 is selected as the liquid composition component taken out from the rectification column, GN2 and LO2 are separated from the raw air, and GO2 obtained from the LO2 is supplied to the consumer. However, the present invention is not limited to this, and in addition to the above-mentioned O2, for example, LN2 may be taken out as a liquid composition component from the tray 34 of the rectification column and supplied to the consumer as a product. Furthermore, the arrangement may be such that argon is separated from the raw material air in liquid form and supplied to the consumer.

Ｃ０上記実施例では、ＬＮ２タンク８からのＬＮ２を精
溜塔３の下塔３１頂部に供給するようにしているが、こ
れに限らず、例えば膨脹タービン６からの寒冷供給先で
ある精溜塔３の上塔３２中部に供給するように構成して
もよい。C0 In the above embodiment, LN2 from the LN2 tank 8 is supplied to the top of the lower column 31 of the rectifying column 3, but the present invention is not limited to this, and for example, the LN2 is supplied to the rectifying column which is the cold supply destination from the expansion turbine 6. It may also be configured such that it is supplied to the middle part of the upper tower 32 of No. 3.

Ｄ、上記実施例におけるポンプ５１をＬＯ２タンク５の
下流側ではなく、例えば上流側である導管５００に介在
させ、このポンプによってタンク５内の圧力を上げるこ
とにより、内部のＬＯ２を送給させるようにしてもよい
。D. The pump 51 in the above embodiment is placed not on the downstream side of the LO2 tank 5, but for example in the conduit 500 on the upstream side, and by increasing the pressure inside the tank 5 with this pump, the internal LO2 is supplied. You may also do so.

Ｅ、また需要先で要求されるＧＯ２などの圧力が比較的
低い場合には第１図などに示すポンプ５１を省略しても
よい。この場合には精溜塔３から導管５００を通して取
出される際のＬＯ２の圧力によって需要先まで送給すれ
ばよい。Furthermore, if the pressure of GO2 or the like required by the customer is relatively low, the pump 51 shown in FIG. 1 may be omitted. In this case, the pressure of LO2 taken out from the rectification column 3 through the conduit 500 may be used to deliver it to the consumer.

〔発明の効果〕〔Effect of the invention〕

この発明の請求項１の空気分離装置によれば、空気分離
手段の定常運転を継続しつつ、供給手段によって製品ガ
スの供給を需要先での需要変動に対応して行うことがで
きる。しかも供給に際し、液状組成成分の冷熱エネルギ
ーを精留塔から取出したＧＮ２の液化に有効利用するこ
とができ、これにより得られるＬＮ２を空気分離手段で
の寒冷源として利用することにより、上記供給手段を設
けない場合に比べて空気分離手段での液化分離に伴う動
力消費を軽減することができる。According to the air separation apparatus of claim 1 of the present invention, the supply means can supply the product gas in response to demand fluctuations at the demand site while continuing the steady operation of the air separation means. Moreover, during supply, the cold energy of the liquid composition components can be effectively used to liquefy the GN2 taken out from the rectification column, and the LN2 obtained thereby can be used as a cold source in the air separation means, thereby reducing the amount of heat generated by the supply means. The power consumption associated with liquefaction separation by the air separation means can be reduced compared to the case where no air separation means is provided.

請求項２の構成によれば、一つの空気分離手段に対して
一つの供給手段を組合せる場合と比べて装置をコンパク
トにすることができる。According to the configuration of claim 2, the apparatus can be made more compact than when one supply means is combined with one air separation means.

請求項３の構成によれば、需要先としての製鉄所などか
ら必要とされるＧ　Ｏ２を、その需要変動に対応して確
実に供給することができる。According to the configuration of claim 3, GO2 required by a steel mill or the like as a demand destination can be reliably supplied in response to demand fluctuations.

請求項５の構成によれば、寒冷発生手段を空気分離手段
側に設ける必要がなく、装置全体を簡易に構成すること
ができる。According to the configuration of claim 5, there is no need to provide the cold generation means on the air separation means side, and the entire apparatus can be configured simply.

【図面の簡単な説明】[Brief explanation of drawings]

第１図はこの発明の第１実施例を示す説明図、第２図は
第２実施例を示す説明図、第３図は第３実施例を示す説
明図、第４図は第４実施例を示す説明図、第５図は従来
の空気分離装置を示す説明図、第６図（よ従来の課題を
解決するために考えられる構成を示す説明図である。 ２・・・主熱交換器、３・・・精溜塔、５・・・ＬＯ２
タンク、６ａ・・・膨脹タービン、７・・・蒸発器、８
・・・ＬＮ２タンク、１１・・・空気圧縮機、１２・・
・Ｎ２圧縮機、Ａ・・・空気分離手段、Ｂ・・・供給手
段。 第　　５ 図 特許出願人　　　　　　株式会社神戸製鋼所代　理　人
　　　　　　　弁理士　小谷悦司同　　　　　　　　　
弁理士　長１）正向　　　　　　　　　弁理士　伊藤孝
夫Ｃ′Fig. 1 is an explanatory diagram showing a first embodiment of the invention, Fig. 2 is an explanatory diagram showing a second embodiment, Fig. 3 is an explanatory diagram showing a third embodiment, and Fig. 4 is an explanatory diagram showing a fourth embodiment. FIG. 5 is an explanatory diagram showing a conventional air separation device, and FIG. 6 is an explanatory diagram showing a possible configuration for solving the conventional problems. 2... Main heat exchanger , 3... Rectification tower, 5... LO2
Tank, 6a... Expansion turbine, 7... Evaporator, 8
...LN2 tank, 11...Air compressor, 12...
- N2 compressor, A...air separation means, B...supply means. Figure 5 Patent applicant Kobe Steel Co., Ltd. Representative Patent attorney Etsushi Kotani
Patent Attorney Chief 1) Masamukai Patent Attorney Takao Ito C'

Claims (1)

【特許請求の範囲】 １、空気圧縮機と、この空気圧縮機により取入れた原料
空気を冷却する主熱交換器と、冷却された原料空気から
選択的に組成成分を液状で分離する精溜塔とを有する空
気分離手段からなる空気分離装置において、上記空気分
離手段には上記液状組成成分を気化させて需要先に供給
する供給手段が設けられ、この供給手段は上記液状組成
成分を蓄えるように上記精溜塔と接続された組成成分タ
ンクと、上記精留塔での分離過程で生成された窒素を上
記組成成分タンクから取出した液状組成成分によって冷
却する第２の熱交換器と、この第２の熱交換器によって
液化された窒素を蓄える液体窒素タンクとが備えられ、
この液体窒素タンクと精溜塔とは上記液体窒素タンク内
の液体窒素を精溜塔に供給可能になるように互いに接続
されていることを特徴とする空気分離装置。 ２、複数の空気分離手段と、一つの供給手段とによって
構成されることを特徴とする請求項１記載の空気分離装
置。 ３、液状組成成分が液体酸素であることを特徴とする請
求項１または請求項２記載の空気分離装置。 ４、液体窒素タンクからの液体窒素が精溜塔に寒冷源と
して供給されるように構成されていることを特徴とする
請求項１〜３のいずれかに記載の空気分離装置。 ５、空気分離手段と供給手段とで必要なすべての寒冷を
発生する寒冷発生手段を上記供給手段側に設けたことを
特徴とする請求項１〜４のいずれかに記載の空気分離装
置。[Claims] 1. An air compressor, a main heat exchanger that cools the feed air taken in by the air compressor, and a rectification column that selectively separates constituent components in liquid form from the cooled feed air. In the air separation device comprising an air separation means, the air separation means is provided with a supply means for vaporizing the liquid composition component and supplying it to a consumer, and the supply means stores the liquid composition component. a component tank connected to the rectification column; a second heat exchanger that cools nitrogen generated in the separation process in the rectification column by the liquid component taken out from the component tank; a liquid nitrogen tank for storing nitrogen liquefied by the heat exchanger No. 2;
An air separation device characterized in that the liquid nitrogen tank and the rectification column are connected to each other so that the liquid nitrogen in the liquid nitrogen tank can be supplied to the rectification column. 2. The air separation device according to claim 1, comprising a plurality of air separation means and one supply means. 3. The air separation device according to claim 1 or 2, wherein the liquid composition component is liquid oxygen. 4. The air separation apparatus according to any one of claims 1 to 3, wherein the air separation apparatus is configured so that liquid nitrogen from the liquid nitrogen tank is supplied to the rectification column as a cold source. 5. The air separation device according to any one of claims 1 to 4, characterized in that a cold generation means for generating all the cold necessary for the air separation means and the supply means is provided on the side of the supply means.
JP2164686A 1990-06-22 1990-06-22 Air separating device Pending JPH0455682A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2164686A JPH0455682A (en) 1990-06-22 1990-06-22 Air separating device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2164686A JPH0455682A (en) 1990-06-22 1990-06-22 Air separating device

Publications (1)

Publication Number Publication Date
JPH0455682A true JPH0455682A (en) 1992-02-24

Family

ID=15797930

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2164686A Pending JPH0455682A (en) 1990-06-22 1990-06-22 Air separating device

Country Status (1)

Country Link
JP (1) JPH0455682A (en)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0842385B2 (en) † 1995-07-21 2003-12-03 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized gaseous product
JP2005273959A (en) * 2004-03-23 2005-10-06 Kobe Steel Ltd Low-temperature air separating apparatus and method operating the same
JP2007502964A (en) * 2003-05-28 2007-02-15 レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・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 Method and arrangement for back-up supply of pressurized gas by cryogenic liquid spray
JP2010032129A (en) * 2008-07-29 2010-02-12 Air Water Inc Air separator
CN105823302A (en) * 2016-05-18 2016-08-03 杭州杭氧股份有限公司 Air separation device and method capable of achieving oxygen inner and outer compression procedure interchange
FR3062197A3 (en) * 2017-05-24 2018-07-27 Air Liquide METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION
FR3119225A1 (en) * 2021-01-27 2022-07-29 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for the emergency supply of a gas

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4945998A (en) * 1972-09-11 1974-05-02
JPS5242158A (en) * 1975-09-30 1977-04-01 Yokogawa Hokushin Electric Corp Device for measuring breaking time of relay

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4945998A (en) * 1972-09-11 1974-05-02
JPS5242158A (en) * 1975-09-30 1977-04-01 Yokogawa Hokushin Electric Corp Device for measuring breaking time of relay

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0842385B2 (en) † 1995-07-21 2003-12-03 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized gaseous product
JP2007502964A (en) * 2003-05-28 2007-02-15 レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・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 Method and arrangement for back-up supply of pressurized gas by cryogenic liquid spray
JP2005273959A (en) * 2004-03-23 2005-10-06 Kobe Steel Ltd Low-temperature air separating apparatus and method operating the same
JP2010032129A (en) * 2008-07-29 2010-02-12 Air Water Inc Air separator
CN105823302A (en) * 2016-05-18 2016-08-03 杭州杭氧股份有限公司 Air separation device and method capable of achieving oxygen inner and outer compression procedure interchange
CN105823302B (en) * 2016-05-18 2018-12-28 杭州杭氧股份有限公司 It is a kind of to be able to achieve the air-separating plant and method that compression process exchanges inside and outside oxygen
FR3062197A3 (en) * 2017-05-24 2018-07-27 Air Liquide METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION
FR3119225A1 (en) * 2021-01-27 2022-07-29 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for the emergency supply of a gas

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