JPH02293575A - Air separation device - Google Patents

Air separation device

Info

Publication number
JPH02293575A
JPH02293575A JP11565189A JP11565189A JPH02293575A JP H02293575 A JPH02293575 A JP H02293575A JP 11565189 A JP11565189 A JP 11565189A JP 11565189 A JP11565189 A JP 11565189A JP H02293575 A JPH02293575 A JP H02293575A
Authority
JP
Japan
Prior art keywords
air
liquid
tank
air separation
supplied
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
JP11565189A
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 JP11565189A priority Critical patent/JPH02293575A/en
Publication of JPH02293575A publication Critical patent/JPH02293575A/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
    • F25J3/04763—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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04006—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
    • F25J3/04151—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
    • F25J3/04339—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 air
    • F25J3/04345—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 air 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
    • F25J3/04406—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
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—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

Abstract

PURPOSE:To effectively utilize cold/heat energy of liquid composition components and to alleviate power consumption upon separation of liquid by air separating means by liquefying the air by cold/heat energy of the composition component, and feeding the liquefied air to a refining tower as material air and cold source. CONSTITUTION:Air separating means A of an air separator is composed of a first air compressor 11, a main heat exchanger 2, a refining tower 3 for separating LN2 and LO2 from the air, and an expansion turbine 6. Supply means B is composed of a LN2 tank 4, a LO2 tank 5, output pumps 41, 51, a second air compressor 12, an evaporator 7 for thermally exchanging product LN2, product LO2 with the air, and a liquid air tank 8. In the evaporator 7, the LN2, LO2 from conduits 411, 511 are thermally exchanged with the air from a conduit 120, the LN2, LO2 are gasified, and supplied to a demand destination as products GN2, GO2. The air is liquefied, stored in a liquid air tank 8, supplied to a refining tower 3, and utilized as material air and as part of cold source in case of separating.

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２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. 2, 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（１−１２０
＞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 in the feed air (1-120
>, carbon dioxide (CO2), etc. are adsorbed and removed, and the remaining pretreated raw air is sent to the main heat exchanger 2 in the cryogenic section C.
sent to. 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ＮＭ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 NM column 3 is composed of a lower column 31, an upper column 32, and a main evaporator 33 that exchanges heat between them. 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
間に遠流ＬＮ２と接触し、しだいにそのＮ２ｍ１度が高
められ、下塔３１ｍ’ｉ部では高純度Ｎ２となる。この
Ｎ２は主蒸発＆Ｉ３３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 the far-flow LN2 while rising in the lower column 31, and its N2ml degree is gradually increased, becoming high purity N2 in the lower column 31m'i section. This N2 enters the main evaporator &I 33, exchanges heat with LO2 in the upper column 32, and condenses to become LN2. This LN2 is
A part of the reflux liquid is supplied 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ｏ２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 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 O2 concentration is increased, and the liquid air containing about 40% O2 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６３３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ＧＯ２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 condensed and high-purity LO2 accumulates at the bottom of the upper column 32, and this LO2 is gasified by heat exchange with the N2 from the evaporation 633, and then taken out as gaseous oxygen (hereinafter referred to as GO2) through the conduit 320. . This GO2 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, and after cooling the raw material air in the main heat exchanger 2, it is used as a product gas nitrogen. The product is supplied to customers as "Product GN2" hereinafter.

また上記ＬＮ２　、ＬＯ２の分離精製のための寒冷は、
膨脹タービン６によって原料空気の一部を断熱膨脹させ
て発生させ、これを精溜塔３の上塔３２中部に専管６０
０を通して供給している。In addition, the refrigeration for separation and purification of LN2 and LO2 is
A part of the raw material air is adiabatically expanded and generated by the expansion turbine 6, and is passed through a dedicated pipe 60 to the middle of the upper column 32 of the rectification column 3.
It is supplied through 0.

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する必要がある。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Ｇｏ２が得られるために、需要先での需要に応じてそ
の運転を途中で停止したり変ｉｌｌざせたりすることは
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 etc. intermittently. However, in the above-mentioned air separation means, since the product GN2 and the product Go2 of almost constant purity can be obtained by continuing operation in a steady state, the operation may be stopped midway depending on the demand at the customer. You cannot change or change it.

このため従来は、第２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′ｌｌ続運転により製造された製品
ＧＯ２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Ｇ０２゛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 etc. has been provided between the air separation means shown in FIG. 2 and the consumer. in this case,
The product GO2 and the like produced by the continuous operation of the air separation means are stored under high pressure in the gas holder H, and the product G02 and the like are supplied from the gas holder H to the customer 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■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
ＧＯ２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, when the above-mentioned gas holder ■ is installed as a supply means, a relatively large capacity gas holder is required because the product GO2 is stored in the gas holder even when the supply to the demand destination is stopped. becomes. 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３図
に示すように供給手段として製品ＬＮ２タンク４や製品
ＬＯ２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の一部が製品しＮ２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＠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ＬＯ２タンク５に取出される。そしてこの製品ＬＮ
２タンク４や顎品ＬＯ２タンク５からは、１Ｎ２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ＬＯ２は蒸発器４０．５０に
よってガス化され、製品ＧＮ２や製品ＧＯ２として霊要
先に供給される。In order to make the air separation device compact, a product LN2 tank 4 and a product LO2 tank 5 are provided as supply means as shown in Fig. 3, and N2 and 02 are supplied to these tanks in a liquid state rather than a gas state. 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 N2 through the conduit 400 to the product LN2 tank 4, and also to the upper column 3 of the rectifier @3.
2 bottom LO2 is taken out through conduit 500 to product LO2 tank 5 as product Lo2. And this product LN
From 2 tank 4 and jaw goods LO2 tank 5, 1N2 and LO
2 is taken out by a pump 41.51 in response to demand from a consumer, and this LN2 and LO2 are gasified by an evaporator 40.50 and supplied to a spiritual destination as product GN2 and product GO2.

ところが第３図に示す供給手段と空気分離手段とを組谷
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１０２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 structure shown in FIG. 3 in which the supply means and the air separation means are combined in a valley, product LN2 and product LO2 exchange heat with the atmosphere and hot water in the evaporator 40.50. The cold energy possessed by 102 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〕 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
を冷却する主篇交換器と、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、空気圧縮機によって取入れた空気を上記組成成分タ
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空
気を蓄える液体空気タンクとが備えられ、この液体空気
タンクと精溜塔とは上記液体空気タンク内の液体空気が
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。(Means for Solving the Problems) In order to achieve the above object, claim 1 of this invention:
It consists of an air separation means having an air compressor, a main exchanger that cools the raw material air taken in by the air compressor, and a rectification column that selectively separates constituent components in liquid form from the cooled raw material 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 the air taken in by the air compressor with the liquid component taken out from the component tank, and liquid air that stores the air liquefied by the second heat exchanger. The liquid air tank and the rectification tower are connected to each other so that the liquid air in the liquid air tank can be supplied to the rectification tower.

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、組成成分として、窒素および酸素のいず
れか一方、または双方を選択して原料空気から分離する
ように構成した。In the third aspect of the present invention, one or both of nitrogen and oxygen is selected as a composition component and separated from the raw air.

請求項４では、液体空気タンクからの液体空気が精溜塔
に原料空気として供給されるように構成した。According to a fourth aspect of the present invention, the liquid air from the liquid air tank is supplied to the rectification column as raw air.

請求項５では、液体空気タンクからの液体空気が精溜塔
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 5, the liquid air from the liquid air tank is supplied to the rectification column as a cold source for separation.

請求項６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 sixth 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） 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空気が液
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。さらに液化された空気を原料空気および寒
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。(Function) According to the structure of claim 1, since the air is liquefied by the cold energy of the liquid component taken out from the component tank, the cold energy can be effectively utilized. Furthermore, by sending the liquefied air to the rectification tower as raw air and a cold source, the power required to generate 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） 第１図において、空気分離＊＠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、第１の空
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Ｌｏ２を分離する精溜塔３と、寒冷を
発生させる膨脹タービン６とから基本構成されている。(Example) In FIG. 1, air separation *@ is composed of air separation means A and supply means B. The air separation means A includes a first 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 separates LN2 and Lo2 from the feed air. It basically consists of a rectification column 3 that generates cooling, and an expansion turbine 6 that generates refrigeration.

また供給手段Ｂは、製品ＬＮ２を蓄えるＬＮ２タンク４
と、製品ＬＯ２を蓄える製品ＬＯ２タンク５と、それぞ
れのタンク４．５から製品ＬＮ２や液体ＬＯ２を取出す
ポンプ４１．５１と、第２の空気圧縮機１２と、上記製
品上Ｎ２や製品ＬＯ２とこの第２の空気圧縮機１２によ
って取入れた空気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空
気を蓄える液体空気タンク８とから基本構成されている
。In addition, the supply means B includes an LN2 tank 4 that stores the product LN2.
, a product LO2 tank 5 that stores product LO2, a pump 41.51 that extracts product LN2 and liquid LO2 from each tank 4.5, a second air compressor 12, and a product LO2 tank 5 that stores the product LO2 and the product LO2. An evaporator (second
It basically consists of a heat exchanger) 7 and a liquid air tank 8 that stores the air liquefied by the evaporator 7.

上記空気分離手段八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（Ｈ２
　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 pretreatment adsorption tower in the air separation means 8 consists of a pair of adsorbers, one of which is used to extract moisture (H2
0) and carbon dioxide <CO2), while adsorbing and removing
The other adsorber is configured to be regenerated with relatively low purity N2 from rectification column 3.

上記第１の空気圧縮機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ｌｉｌｌｌｉ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 first 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 lilli column 3 through a conduit 111.
It is connected to the lower part of the lower tower 31. 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と導管４００との一端が接続されている。一方の導管
３１１は上塔３２上部に接続され、他方の導管４００は
製品ＬＮ２タンク４と接続されている。また下塔３１底
部と上塔３２中部とは導管３１２によって接続されてい
る。また上記上塔３２頂部は導管３２１によって主熱交
換器２と接続されている。また上塔３２底部には導管５
００の一端が接続され、この導管５００はＬＯ２タンク
５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 and a conduit 400 are connected at one end. One conduit 311 is connected to the upper part of the upper tower 32, and the other conduit 400 is connected to the product LN2 tank 4. Further, the bottom of the lower tower 31 and the middle part of the upper tower 32 are connected by a conduit 312. Further, the top of the upper column 32 is connected to the main heat exchanger 2 through a conduit 321. Also, at the bottom of the upper tower 32 is a conduit 5.
00 is connected, and this conduit 500 is connected to the LO2 tank 5.

また主熱交換器２内でｗ＃管１１０が分岐され、この分
岐管６００は膨服タービン６を介在して精溜塔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ｙｇ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。Further, the w# pipe 110 is branched within the main heat exchanger 2, and this branch pipe 600 is connected to the middle part of the upper column 32 of the rectification column 3 via the expansion turbine 6. Further, a YG pipe (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. There is.

ＬＮ２タンク４およびＬＯ２タンク５にはポンプ４１．
５１が接続され、このポンプ４１．５１は導管４１１，
５１１によってＬＮ２やＬＯ２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ＧＮ２や製
品ＧＯ２が転炉や電気炉などを有する製鉄所ＬＫＩ要先
》まで送給可能に導管４１２．５１２にようて上記需要
先と接続されている。The LN2 tank 4 and the LO2 tank 5 are equipped with a pump 41.
51 is connected, and this pump 41.51 is connected to the conduit 411,
511, it is connected to the evaporator 7 so that LN2 and LO2 can be sent, and this evaporator 7 can send the gasified products GN2 and GO2 to the LKI destination of the steelworks that has converters, electric furnaces, etc. It is connected to the above-mentioned customer through conduits 412 and 512.

また第２の空気圧縮機１２は導管１２０によって蒸発器
７と接続され、この蒸発器７は液化された液体空気を送
給可能に導管１２１によって液体空気タンク８と接続さ
れている。さらにこの液体空気タンク８には導管１２２
の一端がｍ続され、この導管１２２の他端は液体空気を
送給可能に精溜塔３の下塔３１中部と接続されている。The second air compressor 12 is also connected by a conduit 120 to an evaporator 7, which is connected to a liquid air tank 8 by a conduit 121 so as to be able to supply liquefied liquid air. Furthermore, this liquid air tank 8 has a conduit 122.
One end of the conduit 122 is connected to the other end of the conduit 122, and the other end of the conduit 122 is connected to the middle part of the lower column 31 of the rectification column 3 so as to be able to supply liquid air.

なお上記導管１２０には、図示しない第２の前処理用吸
着塔が介在されている。Note that a second pretreatment adsorption tower (not shown) is interposed in the conduit 120.

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ｌｌ１１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（Ｈ２　０）
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
ｌ管１１０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１
１１を通して精溜塔３の下塔３１に入れられる。The raw air is compressed by a first air compressor ll11,
Moisture (H20) in the raw air is removed by an adsorption tower (not shown).
Carbon dioxide (CO2) and the like are adsorbed and removed, and the remaining pretreated raw material air is sent to the main heat exchanger 2 in the cryogenic section C through the l pipe 110. In this main heat exchanger 2, the feed air is cooled to near its boiling point, and then
11 into the lower column 31 of the rectification column 3.

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ＬＮ２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ＵＮ２となる。このＮ２は
主蒸発器３３に入り．Ｌ塔３２のＬＯ２と熱交換して凝
抛することにより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、他の一部がｙＩＪｔ１４００を通してＬＮ２タ
ンク４に送られ、また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 the reflux LN2 while rising in the lower column 31, and its N2 concentration is gradually increased, becoming highly pure UN2 at the top of the lower column 31. This N2 enters the main evaporator 33. It exchanges heat with LO2 in the L 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, another portion is sent to the LN2 tank 4 through the yIJt1400, and the remainder is returned to the top of the lower column 31 as a reflux liquid.

この還流液は下Ｗ１３１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ｏ２ｍ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３
１底部から取出されて上塔３２中部に尋管３１２を通し
て供給される。While this reflux liquid goes down the lower W131, this lower tower 31
The o2m temperature is increased by contact with the raw material air rising inside, and is stored at the bottom of the lower column 31 as liquid air containing about 40% O2. And this liquid air is in the lower tower 3
1 is taken out from the bottom and supplied to the middle of the upper tower 32 through a fathom tube 312.

この液体空気は、上塔３２中部から．下方に流れる間に
０２が濃縮されて上塔３２底部には高純度のＬＯ２が溜
り、このＬＯ２の一部は蒸発器３３でＮ２と熱交換して
ＬＯ２は蒸発してＧＯ２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１０
２は導管５００を通して取出され、ＬＯ２タンク５に蓄
えられる。This liquid air is supplied from the middle of the upper tower 32. While flowing downward, 02 is concentrated and high purity LO2 accumulates at the bottom of the upper column 32. A part of this LO2 exchanges heat with N2 in the evaporator 33, and LO2 evaporates to become GO2, which is then transferred to the upper column. The gas rises in the rectification column at 32 and undergoes a rectification operation. remaining 10
2 is removed through conduit 500 and stored in LO2 tank 5.

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Ｂ２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。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 B2 through a conduit 321, where the main heat exchanger 2 cools the feed air.

また第１の空気圧縮機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で断熱膨服されて
寒冷が発生され、これを精溜塔３の上塔３２中部に導管
６００を通して供給される。In addition, a part of the raw air sent to the main heat exchanger 2 by the first air compressor 12 is adiabatically expanded by the expansion turbine 6 to generate cold, which is transferred to the middle part of the upper column 32 of the rectification column 3. It is fed through conduit 600.

供給手段Ｂでは、ポンプ４１．５１の作動により需要先
からの需要に応じてＬＮ２やＬＯ２が蒸発器７に導管４
１１．５１１を通して送られる。In the supply means B, LN2 and LO2 are supplied to the evaporator 7 through the conduit 4 according to the demand from the customer by operating the pumps 41 and 51.
11. Sent through 511.

一方、第２の空気圧縮ｌ１１２も上記需要に応じて作動
され、これにより空気が取入れられ、この空気は図示し
ない第２の前処理用吸着塔により前処理された後、蒸発
器７に々管１２０を通して送られる。On the other hand, the second air compressor 112 is also operated according to the above demand, thereby taking in air. After being pretreated by a second pretreatment adsorption tower (not shown), this air is piped to the evaporator 7. 120.

この蒸発器７では導管４１１．５１１からのＬＮ２およ
びＬＯ２と、導管１２０からの空気とが熱交換される。In this evaporator 7, heat is exchanged between LN2 and LO2 from conduit 411.511 and air from conduit 120.

これによって上記ＬＮ２やＬＯ２はガス化され、製品Ｇ
Ｎ２や製品ＧＯ２として需要先に導管４１２．５１２を
通して供給される。As a result, the above LN2 and LO2 are gasified, and the product G
It is supplied to customers as N2 and product GO2 through conduits 412 and 512.

また、上記空気は上記ＬＮ２などによって冷却されて液
化し、液体空気が導管１２１を通して液体空気タンク８
に蓄えられる。この液体空気タンク８の液体空気は、連
続運転されている空気分離手段Ａの精溜塔３へ導管１２
２を通してその下塔３１中部に一定流量供給される。こ
れによって上記液体空気は導管１１１から供給される原
料空気とともに原料空気として利用され、また分離に際
する寒冷源の一部としても利用される。Further, the air is cooled and liquefied by the LN2, etc., and the liquid air passes through the conduit 121 to the liquid air tank 8.
is stored in The liquid air in the liquid air tank 8 is passed through a conduit 12 to the rectification column 3 of the air separation means A which is continuously operated.
A constant flow rate is supplied to the middle part of the lower column 31 through 2. As a result, the liquid air is used as raw material air together with the raw material air supplied from the conduit 111, 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脹タービン
６からの寒冷の他に、導管１２２を通して供給手段Ｂか
ら液体空気としての寒冷が精溜塔３に供給されるために
、この液体空気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 liquid air is supplied to the rectification column 3 from the supply means B through the conduit 122, so that if this liquid air is not supplied, Compared to this, 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.

さらに従来の供給手段としてガスホルダーを用いる場合
に比べて、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 is used as a conventional supply means, since the gas can be stored in a liquid state, the entire device can be made more compact.

第４図には第２実施例が示されている。これは供給手段
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第２の空気圧縮機１２か
らの空気の一部を断熱膨脹させて寒冷を発生させ、この
寒冷を蒸発器７での空気の液化を促進し、ここで得られ
る寒冷を液体空気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
寒冷などが上記膨脹タービン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る。A second embodiment is shown in FIG. This is achieved by installing an expansion turbine (cold generation means) 6a in the evaporator 7 of the supply means B, which adiabatically expands a part of the air from the second air compressor 12 to generate cold; The evaporator 7 promotes the liquefaction of the air, and the resulting cold air is supplied to the air separation means A in the form of liquid air. As a result, the expansion turbine 6a generates refrigeration necessary for separation in the air separation means A and refrigeration for maintaining low temperature in the supply means B, and thereby the expansion in the air separation means A in the first embodiment The turbine 6 (see FIG. 1) can be omitted.

なお上記第１および第２実施例における他の態様を以下
に説明する。Other aspects of the first and second embodiments will be described below.

Ａ．上記実施例では、一つの空気分離手段八と一つの供
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ＬＮ２やＬＯ２な
どをＬＮ２タンクやＬＯ２タンクなどに蓄えるとともに
、液体空気タンクから複数の精溜塔に液体空気が供給さ
れるように構成すればよい。これによって一つの空気分
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 constituted by one air separation means 8 and one supply means B, but the present invention is not limited to this, and a plurality of air separation devices A. A. ... and one supply means B may constitute an air separation apparatus. 'In this case, LN2, LO2, etc. from a plurality of rectification columns may be stored in an LN2 tank, a LO2 tank, etc., and liquid air may be supplied from a liquid air 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、組成成分としてＮ２とＯ２との２
成分を選択し、原料空気からＬＮ２とＬ０２とを分離し
て需要先に供給するようにしているが、これに限らず、
いずれか一方のみを原料空気から分離して供給するよう
に構成してもよい。B. In the above embodiment, N2 and O2 are used as the composition components.
Although the components are selected and LN2 and L02 are separated from the raw air and supplied to customers, the method is not limited to this.
It may be configured such that only one of them is separated from the raw material air and supplied.

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。さらに、例えば原料空
気からＬＮ２とＧＯ２とに分離してＬＮ２について上記
実施例を適用するようにしてもよい。Furthermore, the arrangement may be such that argon is separated from the raw material air in liquid form and supplied to the consumer. Furthermore, for example, the raw air may be separated into LN2 and GO2, and the above embodiments may be applied to LN2.

Ｃ．上記実施例では、液体空気タンク８からの液体空気
を精溜塔３の下塔３１中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。C. In the above embodiment, the liquid air from the liquid air tank 8 is supplied to the middle part of the lower column 31 of the rectifying column 3, but the present invention is not limited to this. It may be configured to be supplied to the middle part of the upper tower 32 of the tower 3.

Ｄ．上記実施例では空気分離手段Ａと供給手段Ｂとのそ
れぞれに空気圧縮機１１．１２を設けているが、これに
限らず、例えば一つの空気圧縮機によって両手段Ａ．Ｂ
へ空気を分配供給させるように構成してもよい。D. In the above embodiment, air compressors 11 and 12 are provided for each of the air separation means A and the supply means B, but the present invention is not limited to this. B
It may be configured to distribute and supply air to.

Ｅ．上記実施例におけるポンプ４１．５１を第５図に示
すように導管４００，５００に設け、このポンプ４１８
．５１ａによってタンク４．５内の圧力を上げることに
より、内部のＬＯ２　．ＬＮ２を送給させるようにして
もよい。E. The pumps 41, 51 in the above embodiment are provided in the conduits 400, 500 as shown in FIG.
．． By increasing the pressure in tank 4.5 by means of 51a, the internal LO2. LN2 may also be supplied.

Ｆ．また需要先で要求されるＬＮ２などの圧力が比較的
低い場合には第１図，第５図に示すポンプ４１．４１ａ
，５１．５１ａを省略してもよい。F. In addition, if the pressure of LN2 or the like required at the demand site is relatively low, the pump 41.41a shown in Figures 1 and 5
, 51.51a may be omitted.

この場合には精溜塔３から導管４００．５００を通して
取出される際の１０２　．ＬＮ２の圧力によって′ｍ要
先まで送給すればよい。In this case, 102. The pressure of LN2 can be used to feed it to the desired destination.

〔発明の効果〕 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
ーを空気の液化に有効利用することができ、この液体空
気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。[Effects of the Invention] According to the air separation device according to claim 1 of the present invention, the supply means can supply the product gas in response to demand fluctuations at the demand destination while continuing the steady operation of the air separation means. I can do it. Furthermore, during supply, the cooling energy of the liquid composition components can be effectively used to liquefy the air, and by using this liquid air as a cold source in the air separation means, the air Power consumption associated with liquefaction separation in the separation means 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，場合と比べて装置をコンパ
クトにすることができる。According to the structure of claim 2, the apparatus can be made more compact than in the case where 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ＧＯ２などを、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, it is possible to reliably supply GO2 and the like required by a steel mill or the like as a demand destination in response to demand fluctuations.

請求項４の構成によれば、供給手段からの液体空気を原
料空気め一部としても利用することができる。According to the configuration of claim 4, the liquid air from the supply means can also be used as part of the raw material air reservoir.

請求項６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 6, 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 the drawing]

第１図はこの発明の第１実施例を示す説明図、第２図は
従来の空気分離装置を示す説明図、第３図は従来の課題
を解決するために考えられる構成を示す説明図、第４図
は第２実施例を示す説明図、第５図は第１実施例の他の
態様を示す説明図、第６図は上記第１実施例の第５図と
は異なる他の態様を示す説明図である。 ２・・・主熱交換器、３・・・精溜塔、４・・・ＬＮ２
タンク、５・・・ＬＯ２タンク、６ａ・・・膨脹タービ
ン、７・・・蒸発器、８・・・液体空気タンク、１１．
１２・・・空気圧縮機、Ａ・・・空気分離手段、Ｂ・・
・供給手段。FIG. 1 is an explanatory diagram showing a first embodiment of the present invention, FIG. 2 is an explanatory diagram showing a conventional air separation device, and FIG. 3 is an explanatory diagram showing a configuration considered to solve the conventional problems. FIG. 4 is an explanatory diagram showing the second embodiment, FIG. 5 is an explanatory diagram showing another aspect of the first embodiment, and FIG. 6 is an explanatory diagram showing another aspect of the first embodiment, which is different from FIG. 5. FIG. 2... Main heat exchanger, 3... Rectification column, 4... LN2
Tank, 5... LO2 tank, 6a... Expansion turbine, 7... Evaporator, 8... Liquid air tank, 11.
12...Air compressor, A...Air separation means, B...
・Means of supply.

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、空気圧縮機によって取入れた空気を上記組成成
分タンクから取出した液状組成成分によつて冷却する第
２の熱交換器と、この第２の熱交換器によって液化され
た空気を蓄える液体空気タンクとが備えられ、この液体
空気タンクと精溜塔とは上記液体空気タンク内の液体空
気が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、組成成分として、窒素および酸素のいずれか一方、
または双方を選択して原料空気から分離することを特徴
とする請求項１または請求項２記載の空気分離装置。 ４、液体空気タンクからの液体空気が精溜塔に原料空気
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、液体空気タンクからの液体空気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。 ６、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１〜５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 the air taken in by the air compressor with the liquid component taken out from the component tank; and the second heat exchanger. and a liquid air tank for storing air liquefied by the liquid air tank, and the liquid air tank and the rectification tower are connected to each other so that the liquid air in the liquid air tank can be supplied to the rectification tower. An air separation device characterized by: 2. The air separation device according to claim 1, comprising a plurality of air separation means and one supply means. 3. Either nitrogen or oxygen as a composition component,
3. The air separation apparatus according to claim 1, wherein one or both are selected and separated from the raw material air. 4. The air separation apparatus according to any one of claims 1 to 3, wherein the air separation apparatus is configured such that liquid air from the liquid air tank is supplied to the rectification column as raw air. 5. The air separation apparatus according to any one of claims 1 to 3, wherein the air separation apparatus is configured such that liquid air from the liquid air tank is supplied to the rectification column as a cold source. 6. The air separation device according to any one of claims 1 to 5, 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.
JP11565189A 1989-05-08 1989-05-08 Air separation device Pending JPH02293575A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP11565189A JPH02293575A (en) 1989-05-08 1989-05-08 Air separation device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP11565189A JPH02293575A (en) 1989-05-08 1989-05-08 Air separation device

Publications (1)

Publication Number Publication Date
JPH02293575A true JPH02293575A (en) 1990-12-04

Family

ID=14667917

Family Applications (1)

Application Number Title Priority Date Filing Date
JP11565189A Pending JPH02293575A (en) 1989-05-08 1989-05-08 Air separation device

Country Status (1)

Country Link
JP (1) JPH02293575A (en)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0628778A1 (en) * 1993-06-07 1994-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and high pressure gas supply unit for an air constituent consuming installation
JPH07151462A (en) * 1993-09-15 1995-06-16 Air Prod And Chem Inc Method for low temperature separation of compressed materialair for producing high pressured oxygen and nitrogen product
EP0694746A1 (en) * 1994-07-29 1996-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the production of a gas under pressure in variable quantities
EP0842385B2 (en) † 1995-07-21 2003-12-03 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized gaseous product
JP2006522307A (en) * 2003-04-02 2006-09-28 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 apparatus for the supply of gas under pressure
FR2929697A1 (en) * 2008-04-07 2009-10-09 Air Liquide PROCESS FOR PRODUCING VARIABLE GASEOUS NITROGEN AND VARIABLE GAS OXYGEN BY AIR DISTILLATION
JP2010036056A (en) * 2008-07-31 2010-02-18 Chiyoda Kako Kensetsu Kk Heating module and cooling module
EP2400249A1 (en) * 2010-06-25 2011-12-28 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Air separation method and facility for cryogenic distilling
JP2013117371A (en) * 2011-12-01 2013-06-13 L'air Liquide-Sa Pour L'etude & L'exploitation Des Procedes Georges Claude Method of operation of cryogenic air separation unit
JP2013198900A (en) * 2013-05-01 2013-10-03 Chiyoda Kako Kensetsu Kk Cooling module

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS55128754A (en) * 1979-03-28 1980-10-04 Hitachi Ltd Combined rectification column for air separator
JPS5636754A (en) * 1979-09-04 1981-04-10 Canon Inc Debugging system
JPS6380185A (en) * 1986-09-22 1988-04-11 株式会社　大分サンソセンタ− Air liquefying separator proper to fluctuation of demand
JPS63143482A (en) * 1986-12-05 1988-06-15 株式会社日立製作所 Tsa adsorption type air low-temperature separator
JPS63282474A (en) * 1987-05-12 1988-11-18 花王株式会社 Production unit for nitrogen

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS55128754A (en) * 1979-03-28 1980-10-04 Hitachi Ltd Combined rectification column for air separator
JPS5636754A (en) * 1979-09-04 1981-04-10 Canon Inc Debugging system
JPS6380185A (en) * 1986-09-22 1988-04-11 株式会社　大分サンソセンタ− Air liquefying separator proper to fluctuation of demand
JPS63143482A (en) * 1986-12-05 1988-06-15 株式会社日立製作所 Tsa adsorption type air low-temperature separator
JPS63282474A (en) * 1987-05-12 1988-11-18 花王株式会社 Production unit for nitrogen

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5566556A (en) * 1993-06-07 1996-10-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
FR2706195A1 (en) * 1993-06-07 1994-12-16 Air Liquide Method and unit for supplying pressurized gas to an installation consuming an air component.
EP0628778B2 (en) † 1993-06-07 2001-03-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and high pressure gas supply unit for an air constituent consuming installation
EP0628778A1 (en) * 1993-06-07 1994-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and high pressure gas supply unit for an air constituent consuming installation
US5505052A (en) * 1993-06-07 1996-04-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
CN1045656C (en) * 1993-06-07 1999-10-13 乔治·克劳德方法的研究开发空气股份有限公司 Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
JPH07151462A (en) * 1993-09-15 1995-06-16 Air Prod And Chem Inc Method for low temperature separation of compressed materialair for producing high pressured oxygen and nitrogen product
FR2723184A1 (en) * 1994-07-29 1996-02-02 Grenier Maurice PROCESS AND PLANT FOR THE PRODUCTION OF GAS OXYGEN UNDER PRESSURE WITH VARIABLE FLOW RATE
US5526647A (en) * 1994-07-29 1996-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure at a variable flow rate
EP0694746A1 (en) * 1994-07-29 1996-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the production of a gas under pressure in variable quantities
EP0842385B2 (en) † 1995-07-21 2003-12-03 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized gaseous product
JP2006522307A (en) * 2003-04-02 2006-09-28 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 apparatus for the supply of gas under pressure
FR2929697A1 (en) * 2008-04-07 2009-10-09 Air Liquide PROCESS FOR PRODUCING VARIABLE GASEOUS NITROGEN AND VARIABLE GAS OXYGEN BY AIR DISTILLATION
JP2010036056A (en) * 2008-07-31 2010-02-18 Chiyoda Kako Kensetsu Kk Heating module and cooling module
EP2400249A1 (en) * 2010-06-25 2011-12-28 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Air separation method and facility for cryogenic distilling
JP2013117371A (en) * 2011-12-01 2013-06-13 L'air Liquide-Sa Pour L'etude & L'exploitation Des Procedes Georges Claude Method of operation of cryogenic air separation unit
JP2013198900A (en) * 2013-05-01 2013-10-03 Chiyoda Kako Kensetsu Kk Cooling module

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