TWI270644B - Air separator and operating method thereof - Google Patents

Air separator and operating method thereof Download PDF

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Publication number
TWI270644B
TWI270644B TW093131546A TW93131546A TWI270644B TW I270644 B TWI270644 B TW I270644B TW 093131546 A TW093131546 A TW 093131546A TW 93131546 A TW93131546 A TW 93131546A TW I270644 B TWI270644 B TW I270644B
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TW
Taiwan
Prior art keywords
nitrogen
natural gas
lng
liquefied natural
cold
Prior art date
Application number
TW093131546A
Other languages
Chinese (zh)
Other versions
TW200517628A (en
Inventor
Tamotsu Hashimoto
Takashi Oyama
Hitoshi Asaoka
Yoshimi Takiguchi
Junichi Nakagawa
Original Assignee
Kobe Steel Ltd
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Application filed by Kobe Steel Ltd filed Critical Kobe Steel Ltd
Publication of TW200517628A publication Critical patent/TW200517628A/en
Application granted granted Critical
Publication of TWI270644B publication Critical patent/TWI270644B/en

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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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • 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
    • F25J3/04406—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/90—Boil-off gas from storage
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The present invention provides an air separator, which can continue operation and prevent BOG even when NG cannot be delivered, and can fully utilize cold of LNG. A nitrogen circulation cooling mechanism 3 of the air separator (which cools nitrogen gas by using the cold of the LNG and adiabatically expanding it to produce liquid nitrogen) is provided with an LNG cold storage passage 34 leading to an LNG heater 37 via an LNG tank 35a, an LNG pump 35b, and a cold accumulator 34a storing the cold of the LNG, and a cold recovery passage 35 returning to the LNG tank 35a via the LNG tank 35a, the LNG pump 35b, a second LNG utilization heat exchanger 33e, a first LNG utilization heat exchanger 33a, the cold accumulator 34a, and a first nitrogen cold utilization heat exchanger 33c.

Description

、1270644 九、發明說明： 【發明所屬之技術領域】 之二發：，特別係關於利用液化天然氣(以下，稱為_ 及直、軍取自大乳之原料空氣分離為氮與氧的空氣分離 裝置及其運轉方法。 77雕 【先前技術】 如眾所周知，空氣分離裝置係用來將空氣中之氮盘氧 分離取出者，具備由壓縮 〃 丨7脹循裱所構成之寒冷 產生衣置。亦有-空氣分離裝置，除具備此種寒冷產生裝 置外，並藉由利用LNG之冷熱，使空氣之分離，及液能製 =態氧 '液態氮、液態氯等)之製造所需要的壓縮二 大幅地減低。此種空氣分離裝置，公知者之系統圖例如圖 所不。以下，參閱其系統圖之圖1〇來說明此習知例之空 氣分離裝置。 & 圖1 0所示之符號5 0，係習知之空氣分離裝置。在此習 知之空氣分離裝置愔 ， - 未圖不之吸附塔等前處理（去 除水分及二氧化碳等)後的原料氣體，通過 導入至精留塔高壓塔（以下，稱為古茂拉β ..... ° ^ Γ柄馮阿壓精留塔）52Η内。鋏 後’從此高塵精料52Η内之底部將富含氧之液態空氣： 至精留塔低壓塔（以下，稱為低塵精留塔）52L之中腹部，並 且從高壓精料52H之上段將液態氮送至低壓精留塔饥 ，塔頂。低壓精留塔似之塔底液，通過閥53而當作氧製 口〇取出至未圖示之液態氧槽内。 另—方面’該低壓精料52L之塔頂氣體（氮氣），以 1270644 該主熱交換器5 1與該已穿成前#;to & ， 70成刖處理之原料氣體進行熱交換 後，依序通過氮預冷器54、氮冷彻哭以 ★ a 几7部為55、複數段之循環壓 縮機56、及氮冷凝器57而冷凝，然後以液氮分離器…乍 氣液分離。液氮分離器58之氣相成分，通過該氮冷凝器57 及氮冷卻器55送回循環壓縮機56，另—方面液相部分則作 為液態_至空氣分離裝4 5〇。更具體而言，該液態氮 之-部份係通過閥60還原至該高壓精留塔52H 過閥5 9取出至未圖示之液態氮槽内。 該氮預冷器54、氮冷卻器55、及氮冷凝器5?係敎六 換器’通過此等熱交換器，進行LNG(從未圖示之 抽出）與氮氣之熱交換。並且，藉由此熱交換同時、;曰 之升溫及蒸發與氮氣之冷凝。（參料敎獻… (專利文獻1)日本特開2002-295799號公報 【發明内容】 但疋’在上述習知例之空氣分離裝置之情形 述之問題。 i ⑴在天然氣（NG)的需求消失而不再送出之情步，因 沒有供冷卻從循環壓縮機排出之壓縮氣體的中間‘卻媒 體’故不得不停止循環壓縮機之運轉。即，需要反覆循产 壓縮機之停止運轉、與再開始運轉，而無法避免空氣八： 裝置之運轉率之降低。 77 (2)又口 LNG之使用量變動較大，空氣分離裝置需 要配合最小之LNG 4吏用可能量來設計，無法充分有 活用LNG之冷熱。 μ 1270644 (3)再者，藉由運轉停止中之供熱會引起殘留於 槽内之UG氣化，產生自然氣化氣（觸，致使⑽槽之内- 壓上升而造成危險，故必須廢棄LNG槽内之刪，有經濟上 不利之問題。 因此，本發明之目的在於提供一種空氣分離裝置，即 ^抓不再送出，亦能繼續運轉，能防止BGG之產生，並且 能充分有效活用LNG之冷熱；並提供其運轉方法。 』本發明係為了解決上述問題而為者，因此，本發明申 請專利範圍第1項之空氣分離裝置，係具備： 空氣麗縮機’將取自大氣之原料空氣I缩至既定壓力； MS吸附器，供淨化空氣壓縮機所壓縮之壓縮空氣； 上精留塔，將該MS吸附器所淨化之展縮空氣，通過主熱 父換器冷卻後，精留分離為氧與氮；及 乳循環冷卻機構’具有氮循環流路，該流路中設有LNG 利用熱交換器（用來將以該精留塔分離且透過該主熱交換 斋取出並以循環壓縮機I縮之麼縮氮氣，# ln 郃)以及衫脹輪機(用來使該循環壓縮機所排出之壓縮氮氣 絕熱膨脹），其特徵在於： 在該氮循環冷卻機構設置： LNG冷熱蓄熱流路’其經由娜槽、咖泵、用以蓄熱 LNG之冷熱之冷熱蓄熱器而通至UG加溫器；及 … 冷熱回收流路，其經由LNG槽、LNG泵、該lng利用埶 交換器、冷熱蓄熱器、利用該氮循環冷卻機構所產生之= 冷的寒冷熱交換器而回至LNG槽。 、 1270644 ^本毛明申請專利範圍第2項之空氣分離裝置，係在申 請專利範圍第"員之空氣分離裝置中，在該氮循環流路之 该循環壓縮機下游側配設升壓機，俾使以該膨脹輪機驅動 且以該循環壓縮機壓縮的壓縮氮氣之壓力上升。 ^本發明申請專利範圍第3項之空氣分離裝置，係在申 請f利範園第丨項之空氣分離裝置中，從該氮循環流路之 循環塵縮機連通至該膨脹輪機的流路之間，設置裝設有循 每冷凍機之分支流路。 本發明申請專利範圍第4項之空氣分離裝置之運轉方 法，其特徵在於： 當能從LNG槽供應充分量之LNG時，與LNG之冷熱所 作用之壓縮氮氣之冷卻並行，使LNG之冷熱蓄熱於冷熱蓄 熱夯，蓄熱後之LNG以LNG加熱器氣化來製造天然氣； 另方面’當能從LNG槽供應之LNG之供應量少時， 以從LNG槽經由LNG泵供應之LNG之冷熱來冷卻壓縮氮氣， 並使該LNG升溫，將一部份或全部氣化的該LNG或NG，合 流於從LNG槽經由LNG泵供應之LNG，使其成為^阢之2相 机後’使其流入該冷熱蓄熱器使2相流之lng液化，來回 收冷熱，並且將冷熱回收後之LNG送回至該LNG槽。 本發明申請專利範圍第5項之空氣分離裝置之運轉方 法，係在申請專利範圍第4項之空氣分離裝置之運轉方法 中，在將該冷熱回收後之LNG送回至LNG槽之前，利用氮 循環冷卻機構所產生之寒冷來冷卻。 依本發明申請專利範圍第丨項至第3項之空氣分離裝 -1270644 置’或本發明申請專利範圍第4項或第5項之空氣分離裝 置之運綠古、1 ' +力法，當NG之需要較多之情形，與LNG之冷熱之 结熱亚订’使循環壓縮機所壓縮之壓縮氮氣以LNG之冷熱 來〜#而施實施液態氮之製造運轉。又，即使NG之需求 $肖十主J[彡 月 藉由利用蓄熱於冷熱蓄熱器之冷熱，能繼續 循％壓縮機之運轉。因此，與習知之空氣分離裝置不相同， 因即徒 Ν Γ @ 4> 、/ 雨求消失而不再送出，仍能繼續運轉，故能提 向空氣分離裝置之運轉率，能有助於提高液態氮之生產 力又因將回至LNG槽之LNG以氮循環冷卻機構所產生 之养~過冷部，而回至LNG槽，藉此使lng槽内之[Μ冷 口p此抑制bog之產生，故不需要廢棄B〇G。 …依本發明申請專利範圍帛2項之空氣分離裝置，在氮 \/瓜路之循J衣壓縮機下游側裝設升壓機，其以膨脹輪機 =動且用以使藉循環壓縮機壓縮的壓縮氮氣之壓力上升。 =此’藉由使更高壓之壓縮氮氣絕熱膨脹，能提高氮循環 =路之液態氮之生產效率。χ，藉由將❹機及膨脹輪機 叹置至少2台’能更提高氮循環流路之液態氮之生產效率。 J本發明申請專利_ 3項之空氣分離裝置，在從 氣循環流路之該循環屬維彡n 叫 衣&細枝連通至該膨脹輪機之流路之 曰’，设置裝設有循環冷凍機所構 /cJ_ m 风刀支/爪路。因藉由將 循％冷凍機設置於氮循環流路 卜 、古旦 此減/循％壓縮機之氮氣 ^，故能提高氮循環流路之液態氮之生產〃 【實施方式】 以下，參閱附圖來說明實施本發明之空氣分離方法的 1270644 空氣分離裝置。円 示意系統圖，圖=之形態1之空氣分㈣置的 料空氣處理部的:Γ明之形態1之空氣分離農置之原 之空氣分離 r . - A 7相（cold box)與液態氮過冷卻邛之、入 -的…統說明圖，目4係本發明之形 二 裝置之氮循環；人各趟 -立/ 工氣为離 之溫度，係在各機 固所纪載 栻时之出入口的LNG或NG之溫度。 本發明之形態i之空氣分離裝置，主要係 個主要部所構成。第1 / “ 文I 1示工軋處理部1，將取 之原料空氣壓縮至既定至壓力，々 料。箆？ 士 Φ W " 了,u i难工乳之原 A卻哭一。 箱2’收容有主熱交換器、精留塔、過 ” ♦。又’第3主要部係氮循環冷卻機構3，將該冷箱1,270644 IX. Description of the invention: [Technical field to which the invention belongs] The second issue: in particular, the use of liquefied natural gas (hereinafter, referred to as _ and straight, the military is taken from the raw material of the milk to separate the air from nitrogen and oxygen. Apparatus and operation method. 77 Engraving [Prior Art] As is well known, an air separation device is used to separate and remove nitrogen in the air, and has a cold-made garment formed by compressing 〃7. In-air separation device, in addition to such a cold generating device, and using the cold heat of LNG to separate the air, and the liquid energy to produce the state of oxygen 'liquid nitrogen, liquid chlorine, etc. Significantly reduced. Such an air separation device is not shown in the system diagram of the known person. Hereinafter, the air separation device of this conventional example will be described with reference to Fig. 1A of the system diagram. & symbol 50 shown in Fig. 10 is a conventional air separation device. In the conventional air separation device, the raw material gas after the pretreatment (removal of water and carbon dioxide, etc.), which is not shown in the adsorption tower, is introduced into the high-pressure tower of the retention tower (hereinafter, referred to as Gumaola β.. ... ° ^ Γ 冯 Feng A pressure retaining tower) 52 Η. After that, 'the bottom of the high dust concentrate 52 将 will be rich in oxygen liquid air: to the lower part of the precision tower low pressure tower (hereinafter referred to as low dust fine retention tower) 52L, and from the upper part of the high pressure concentrate 52H The liquid nitrogen is sent to the low pressure essence to stay hunger, the top of the tower. The bottom liquid of the low pressure retentive column is taken out as an oxygen port through a valve 53 and taken out into a liquid oxygen tank (not shown). In another aspect, the overhead gas (nitrogen gas) of the low pressure concentrate 52L is heat exchanged with the raw material gas of the first heat exchanger 51 and the raw material gas which has been passed through; Then, the nitrogen precooler 54 and the nitrogen refrigerant are chilled by a nitrogen refrigerant, and a plurality of seven, 55, a plurality of cycle compressors 56, and a nitrogen condenser 57 are condensed, and then separated by a liquid nitrogen separator. The gas phase component of the liquid nitrogen separator 58 is returned to the recycle compressor 56 through the nitrogen condenser 57 and the nitrogen cooler 55, and the other liquid phase portion is taken as a liquid_to air separation unit. More specifically, the portion of the liquid nitrogen is reduced by the valve 60 to the high pressure retentate column 52H through the valve 59 to be taken out into a liquid nitrogen tank (not shown). The nitrogen pre-cooler 54, the nitrogen cooler 55, and the nitrogen condenser 5 are connected to the heat exchanger to perform heat exchange between the LNG (not shown) and nitrogen gas. Moreover, by this heat exchange, the temperature rise and the condensation of evaporation and nitrogen gas. (Patent Document 1) Japanese Laid-Open Patent Publication No. 2002-295799 (Summary of the Invention) However, the problem described in the case of the air separation device of the above-described conventional example is as follows: i (1) demand for natural gas (NG) If it disappears and is no longer sent out, there is no need to cool the middle of the compressed gas discharged from the recycle compressor, but the media has to stop the operation of the recycle compressor. That is, it is necessary to repeatedly stop the operation of the compressor. The operation starts again, and air 8 cannot be avoided: the operating rate of the device is reduced. 77 (2) The usage of the LNG is large, and the air separation device needs to be designed with the smallest amount of LNG 4 In addition, the heat of LNG is used. μ 1270644 (3) In addition, the heating in the stop of operation causes gasification of UG remaining in the tank to generate natural gasification gas (touch, causing the inside of the (10) tank to rise. Dangerous, it is necessary to discard the deletion in the LNG tank, which is economically disadvantageous. Therefore, the object of the present invention is to provide an air separation device, that is, it can not continue to be sent, and can continue to operate, thereby preventing the production of BGG. The present invention is directed to solving the above problems. Therefore, the air separation device of claim 1 of the present invention has: air swell The machine 'retracts the air I from the atmosphere to a predetermined pressure; the MS adsorber, which compresses the compressed air compressed by the air compressor; and the upper retentate tower, the contracted air purified by the MS adsorber passes through the main heat After the parent exchanger is cooled, the fine separation is separated into oxygen and nitrogen; and the milk circulation cooling mechanism has a nitrogen circulation flow path, and the flow path is provided with an LNG utilization heat exchanger (for separating and passing the fine retention tower) The main heat exchange is taken out and recirculated by the recycle compressor I, # ln 郃) and the swelled turbine (used to adiabatically expand the compressed nitrogen discharged from the recycle compressor), characterized by: Cooling mechanism setting: LNG hot and cold heat storage flow path, which is connected to the UG warmer via a hot tank and a hot and cold heat accumulator for accumulating LNG; and... a cold heat recovery flow path through the LNG tank and the LNG pump Ln g using a helium exchanger, a hot and cold heat accumulator, and using the cold cold heat exchanger generated by the nitrogen circulation cooling mechanism to return to the LNG tank. 1270644 [The air separation device of the patent application scope 2 of the present invention is In the air separation device of the applicant's patent scope, a booster is disposed on the downstream side of the circulation compressor of the nitrogen circulation flow path to compress the compressed nitrogen driven by the expansion turbine and compressed by the circulation compressor The pressure is increased. The air separation device according to the third aspect of the present invention is in the air separation device of the application of the fifth embodiment, and the circulating dust collecting machine of the nitrogen circulation flow path is connected to the expansion turbine. Between the flow paths, a branch flow path for each chiller is installed. The method for operating an air separation device according to the fourth aspect of the present invention is characterized in that, when a sufficient amount of LNG can be supplied from the LNG tank, the cooling and heat storage of the LNG is performed in parallel with the cooling of the compressed nitrogen by the cold heat of the LNG. In the case of hot and cold heat storage, the LNG after heat storage is gasified by LNG heater to produce natural gas; on the other hand, when the supply of LNG supplied from the LNG tank is small, it is cooled by the cold heat of the LNG supplied from the LNG tank via the LNG pump. The nitrogen gas is compressed, and the LNG is heated up, and the LNG or NG which is partially or completely vaporized is combined with the LNG supplied from the LNG tank via the LNG pump, so that it becomes a camera and then flows into the hot and cold. The heat accumulator liquefies 1 ng of the two-phase flow to recover the cold heat, and returns the LNG after the cold heat recovery to the LNG tank. The operation method of the air separation device according to the fifth aspect of the invention is the operation method of the air separation device according to the fourth aspect of the patent application, wherein the nitrogen is recovered before the LNG is recovered and returned to the LNG tank. The cold generated by the circulating cooling mechanism is cooled. According to the air separation device -1270644 of the present invention, the air separation device of the fourth or fifth aspect of the patent application scope of the present invention, the "1" + force method In the case where there is a large demand for NG, the hot and cold heat of the LNG is combined with the heat of the compressed nitrogen compressed by the circulating compressor to perform the liquid nitrogen production operation. In addition, even if the demand for NG is $10, it can continue to operate according to the % compressor by utilizing the heat and cold stored in the cold and heat accumulator. Therefore, unlike the conventional air separation device, it is possible to continue the operation because the rain is disappeared and is not sent out, so that the operation rate of the air separation device can be improved, which can contribute to improvement. The productivity of liquid nitrogen is returned to the LNG tank by the LNG which is returned to the LNG tank by the nitrogen circulation cooling mechanism, thereby causing the suppression of bog in the lng tank. Therefore, it is not necessary to discard B〇G. According to the air separation device of claim 2 of the present invention, a booster is installed on the downstream side of the nitrogen-/guai road, which is driven by an expansion turbine and is used to compress the borrowing cycle compressor. The pressure of the compressed nitrogen gas rises. = This can increase the production efficiency of the nitrogen cycle of the nitrogen cycle by adiabatic expansion of the higher pressure compressed nitrogen. χ, by slamming the downtime and expansion turbines by at least 2 units, the production efficiency of liquid nitrogen in the nitrogen circulation flow path can be further improved. J. The air separation device of the invention of claim 3, wherein the cycle from the gas circulation flow path is connected to the flow path of the expansion turbine, and the circulation is frozen. Machine structure / cJ_ m wind knife / claw road. Since the nitrogen freezer is installed in the nitrogen circulation flow path and the natural gas is reduced/circulated by the nitrogen gas of the % compressor, the production of liquid nitrogen in the nitrogen circulation flow path can be improved. [Embodiment] The figure illustrates a 1270644 air separation unit embodying the air separation process of the present invention.円 *** *** *** 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态 形态Cooling enthalpy, in- _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ The temperature of LNG or NG. The air separation device of the aspect i of the present invention is mainly composed of main parts. 1 / "I I show the rolling process part 1, the raw material air is compressed to a predetermined pressure, and the material is 箆. Φ 士 W W W W W W W W W W W W W W W W W W W 'Contains the main heat exchanger, the fine tower, and over ♦. Further, the third main part is a nitrogen circulation cooling mechanism 3, and the cold box is

所排出之氮氣壓縮，並且將所壓縮之氮氣以L 換器與膨，輪編bine)予以冷卻來製造液態氮。”、、 “又’第4主要部係、液態氮過冷卻孝g 4，將該氮循環冷卻 機構3所製造之液態氮與低溫之i氣分離，並將液態氮過 冷卻成為液態氮製品。以下，依序參閱圖式，說明構成本 發明之空氣分離裝置的該等主要部之構成。 原料空氣處理部1之構成如圖2所示。即，透過吸取 過濾器11從大氣取入空氣壓縮機12之原料空氣，以此空 氣壓縮機12壓縮至既定壓力例如〇6MPa。從空氣壓縮機 12排出之原料空氣，藉由與冷卻媒體進行熱交換之冷卻器 (cooler)13冷卻後，導入Ms吸附器14，並去除水分及二 氧化碳等。MS吸附器14係構成為並排配設2個，通常係將 ' 1270644 原料空氣導入於任一之Ms吸附器丨4，而將另一之未供使用 之MS吸附器14的未圖示之吸附劑，藉由通過再生電熱器 1 5被加熱之氮氣，使其吸附機能再生後，來轉換使用。 即，藉由交替使用，使空氣分離裝置不必為了 MS吸附 斋14之再生而停止運轉。藉由Ms吸附器丨4去除水分及二 氧化碳等之原料空氣，則透過如圖2所示之流路A送至冷 箱。又，該再生電熱器15，將從收容於後述之冷箱2的低 壓精留塔22並透過圖2所示之流路B所供應的氮氣予以加 熱，藉由經加熱之氮氣供應至MS吸附器14以使吸附劑再 且’使MS吸附器14之吸附劑再生後之氮氣則從消 音裔（silencer)16放出至大氣中。 在該冷箱2内，收容如圖3之左側所示之複數種機器。 此等機器係主熱交換器21、上部之低壓精留塔U、下部之 高，精留塔23、及過冷卻器24。即’在該原料空氣處理： 1處理並透過流路A送至主熱交換器21之 # ,L ^ 4 β工乳，係以 …、父換器21冷卻。又，原料空氣，係藉 iX 99 作稭由從低壓精留 a 22之頂部透過過冷卻器24取出之高 拌匆w Λ 又乳乳、從低壓 精W 22之上部附近透過過冷卻器24取出 (供應至該MS吸附器14) '及從高壓精留塔兩又，氣 度氮氣作熱交換來冷卻。 出之回純 週過該主熱交換器21之冷卻空氣，供應 OQ ^ ^ A ^ 精 之底。卩。供應至此高壓精留塔23之冷卻咖— 斗如叫、， 丨工虱，在塔 功間漸漸變成富含氮，在高壓精留塔23之 純度氮。高純度氮之—部份，從高麼精留、則成 D α以氣體 1270644 通過主無父換裔21加熱而送出系統外。殘留部分則導 引至主冷凝器26，冷卻、冷凝而變成液態氮。被冷凝之液 態氮之一部份，從高壓精留塔23之上部抽出，通過該過冷 部裔24而過冷卻，經減壓後供應至低壓精留塔22之頂部。 歹成餘之液恶氮在塔内流下期間漸漸變成富含氧，當作液態 :氣25積存於咼壓精留塔23之底部。液態空氣25，從高 壓精留塔23抽m過冷卻器、24過冷卻而導入至低壓 精留塔22之中部。 〒二主该低壓精留塔22之中部的富含氧之液態，空氣 、在塔内邊流下邊漸漸冷凝氧，而在底部變成高純度氧。 =，此積存於低壓精留塔22之底部的液態氧，則當作液 恶氧製品取出至系統外。 另-方面，從低壓精㈣22之頂部透過過冷卻器以 取出之南純度氮、及從高壓精留塔23取出之高純度氮，在 =父換器21與原衫氣作熱交換後，透過圖3所示之流 〆D达出，分別送至氮循環冷卻機構3。 氮循環冷卻機構3之構成 氮循環冷卻~ 從流路^送進 路D所導^ 精由氮麼縮機31屢縮至與從流 之氮氣合流，*導；丨至計「 與從流路D導引 出…“ 塵、缩機32。從循環麼縮機犯排 出之鼠乳，係於循環氮循環流路33循 環麼縮機32排出而流經氮 更评5之’從循The discharged nitrogen gas is compressed, and the compressed nitrogen gas is cooled by an L-exchanger and expanded, and the liquid nitrogen is produced. "," and "the fourth main part, liquid nitrogen supercooled filial g 4, the liquid nitrogen produced by the nitrogen circulation cooling mechanism 3 is separated from the low temperature i gas, and the liquid nitrogen is supercooled to a liquid nitrogen product. Hereinafter, the configuration of the main portions constituting the air separation device of the present invention will be described with reference to the drawings. The configuration of the raw material air treatment unit 1 is as shown in Fig. 2 . That is, the raw material air of the air compressor 12 is taken in from the atmosphere through the suction filter 11, and the air compressor 12 is compressed to a predetermined pressure, for example, 〇6 MPa. The raw material air discharged from the air compressor 12 is cooled by a cooler 13 that exchanges heat with a cooling medium, and then introduced into the Ms adsorber 14 to remove moisture, carbon dioxide, and the like. The MS adsorber 14 is configured to be arranged in parallel, usually by introducing '1270644 raw material air into any of the Ms adsorber crucibles 4, and another unapplied adsorption of the unused MS adsorber 14 The agent is converted and used after being regenerated by the nitrogen gas heated by the regenerative heater 15. That is, by alternate use, the air separation device does not have to be stopped for the regeneration of the MS adsorption. The raw material air such as moisture and carbon dioxide is removed by the Ms adsorber 丨4, and then sent to the cold box through the flow path A as shown in Fig. 2. Further, the regenerative electric heater 15 heats the nitrogen gas supplied from the low pressure retentate tower 22 accommodated in the cold box 2, which will be described later, through the flow path B shown in Fig. 2, and supplies it to the MS adsorption by heated nitrogen gas. The nitrogen is then released from the silencer 16 to the atmosphere by the adsorbent and then the nitrogen of the adsorbent of the MS adsorber 14 is regenerated. In the cold box 2, a plurality of machines as shown on the left side of Fig. 3 are housed. These machines are the main heat exchanger 21, the upper low pressure retentate U, the lower portion, the fine column 23, and the subcooler 24. Namely, the #, L ^ 4 β working milk which is treated in the raw material air treatment: 1 and sent to the main heat exchanger 21 through the flow path A is cooled by ..., the parent exchanger 21. Further, the raw material air is taken out from the top of the low-pressure fine retaining a 22 through the subcooler 24 by the iX 99 as a straw, and the milk is taken out from the upper portion of the low-pressure fine W 22 through the subcooler 24 (Supply to the MS adsorber 14) 'And from the high pressure finishing tower, the gas is cooled by heat exchange. The pure cooling air passing through the main heat exchanger 21 is supplied back to the bottom of the OQ ^ ^ A ^ fine. Hey. The cooling coffee supplied to the high-pressure finishing tower 23 is called a bucket, and is completed, and gradually becomes nitrogen-rich in the tower, and the purity nitrogen in the high-pressure finishing tower 23. Part of the high-purity nitrogen, from the high-quality fine, then D α is sent out of the system by heating the gas 1270644 through the main fatherless man. The residual portion is directed to the main condenser 26, cooled and condensed to become liquid nitrogen. A portion of the condensed liquid nitrogen is withdrawn from the upper portion of the high pressure retentate column 23, supercooled by the supercooled portion 24, and supplied to the top of the low pressure retentate column 22 after being depressurized. The liquid nitrogen of the sputum is gradually enriched with oxygen during the flow in the tower, and is regarded as a liquid: the gas 25 is accumulated at the bottom of the smashing tower 23. The liquid air 25 is pumped from the high pressure retentate tower 23 to the subcooler, and is subcooled to be introduced into the middle of the low pressure retentate tower 22. The second part of the low-pressure finishing tower 22 is filled with oxygen-rich liquid, and the air gradually condenses oxygen under the inside of the tower, and becomes high-purity oxygen at the bottom. =, the liquid oxygen accumulated in the bottom of the low pressure retentate tower 22 is taken out of the system as a liquid oxygen product. On the other hand, the high purity nitrogen taken out from the top of the low pressure fine (4) 22 through the subcooler to be taken out and the high purity nitrogen taken out from the high pressure finishing tower 23 are passed through the heat exchange between the parent exchanger 21 and the original shirt gas. The flow D shown in Fig. 3 is reached and sent to the nitrogen circulation cooling mechanism 3, respectively. Nitrogen circulation cooling mechanism 3 is configured to cool nitrogen circulation~ from the flow path ^ delivery path D is refined by the nitrogen reduction machine 31 to merge with the nitrogen gas from the flow, * guide; "to the flow path D" Guided out..." Dust, shrinking machine 32. The rat milk discharged from the circulation machine is discharged from the circulating nitrogen circulation flow path 33 and discharged through the nitrogen and is passed through the nitrogen.

之冷轨之m, .u 33之氮氣’在利用LNG … 利用熱交換器33a冷卻，妳冷卻 部分流至膨脹輪機33b " 虱軋大 、、二知熱知脹之氮氣，則依用以使 12 1270644 LNG過冷卻之第1氮冷熱利用熱交換器33c、用以使未被膨 脹輪機33b分支之殘餘氮液化之第2氮冷熱利用熱交換器 33d、利用LNG之冷熱來冷卻氮之第2LNG利用熱交換器Me 之順序循環。又，第1LNG利用熱交換器33a，係亦使其能6 將吸入於氮壓縮機31之氮氣，吸入於循環壓縮機32之氮 氣冷卻。 又，在該氮循環冷卻機構3設置]LNG冷熱蓄熱流路以， 錢由LNG槽35a、LNG泵35b、用以蓄熱LNG之冷熱之冷 熱蓄熱器、34a而連通至LNG加溫器37。再者，在該氮循環 冷卻機構3設置冷熱回收流路35，其經由[阢槽35&、 泵35b、第2LNG利用熱交換器33e、第利用熱交換哭 33a、冷熱蓄熱器34a、第i氮冷熱利用熱交換器咖而: j LN^曹35a。又，從該冷熱回收流路35之第⑽利用熱 交換器33a出來的部分，使經由預冷器33^別排出流路 36連通至LNG加溫器37。 NG排出流路36與LNG冷熱f熱流路^亦可分別連通 於各LNG加溫器。LNG加溫器37,例如亦可為利用海水之 〇RV(〇Pen Rack Vaporizer)，又亦可為利用循環水之塞發 。又’在此情形，亦可將透過流路C、D吸入_縮機 3!及循《縮機32之氮氣予以預冷的預冷器饥或第脇 利用熱交換器33a、第2LNG利用熱交換器咖、第… =利:熱交換器，、第2氮冷熱利用熱交換器挪各料 為一體化或分割。又，使用於冷熱f熱器…之蓄埶劑之 候補，能列舉如正戍院、正己燒、乙醇、甲基環己烧、卜 13 -1270644 丙醇等。 ， 以該循環壓縮機32壓縮且以該第1LNG利用熱交換器 冷部之氮氣之一部份，如上述般，藉由膨脹輪機33b來 ^脹，但其他氮氣在途中分支而通過第2LNG利用熱交換器 作e、第2氮冷熱利用熱交換器33d之流路β期間被冷卻， 义成液態氮送進圖3所示之液態氮過冷卻箱4來構成。 在該液態氮過冷卻箱4之内部，如圖3之右側所示， 2要係收容氣液分離器41與液態氮過冷卻器42。即，透過 二:E從該氮循環冷卻機構3所供應之液態氮，以氣液分 離2 41分離為低溫之氮氣46與液態氮47。氣液分離器41 :刀離之II氣46之-部份送至低壓精留塔22，殘餘則透過 路F與膨脹輪機33b所排出之氮氣合流。另_方面，液 心㈣氮過冷卻！！ 42使其過冷卻，當作液態氮 衣:取出至系統外。該液態氮47之—部份在氣液分離器Ο 之流出口附近分支而送至高壓精留塔23之頂部。 又’從氣液分離器41之出口將液態氮流路43分支， 透過此《氮流路43使„氮之_料使發㈣氣製品 冷部。在該液態氮流路43,配置根據液態氮溫度檢測 45(用以檢測液態氮製品之液態氮溫度）之檢測溫度 42使液編冷卻。藉此，能製造過冷卻成既定溫度範圍 内之氮製品。 依本發明之形態1之氮循環冷卻_3’能進行下列2 種運轉槽35a供應之lng供應量較多時， 14 1270644 與使用第1、第2LNG利用熱交換器33a、33e之壓縮氮氣之 冷部並行’將LNG供應至LNG冷熱蓄熱流路34而將LNG之 冷熱蓄熱於冷熱蓄熱器34a，並使蓄熱後之LNG以LNG加溫 為37氣化，來製造NG。另一方面，當能從ίΝ(ϊ槽35&供應 之LNG供應量較少時，以從LNG槽35a透過LNG泵3讣供 應至冷熱回收流路35的LNG之冷熱來冷卻壓縮氮氣，將本 身升溫而使一部份或全部氣體化之此LNG或NG，合流於從 L&NG槽35a透過LNG泵35b供應之LNG，使其成為氣液2相 抓。又，藉由使此LNG之氣液2相流流入該冷熱蓄熱器34a， 使氣液2相流液化來回收冷熱，並將冷熱回收後之[μ以 第氮々熱利用熱父換态33c冷卻而送回至LNG槽35a。 又，在此情形，雖利用使其絕熱膨脹之氮氣之冷熱，惟亦 可利用例如氮循環冷卻機構3所得之液態氮之冷熱。 依本發明之形態丨之空氣分離裝置，能獲得如下之效 果。 (1) 即使NG之需求消失而不再送出之情形，藉由將 LNG t、應至冷熱回收流㉟35來循環’能將循環壓縮機π所 排出之壓縮氮氣冷卻。即，因不需要如習知使循環壓縮機 之運轉彳τ止，不拘NG之需要量多少能繼續運轉，故能提 咼空氣分離裝置之運轉率。 (2) 又，即使LNG之使用量變化大，因不需要將空氣 分離裝置配合最小t LNG使用可能量來設計，故能充:有 效活用LNG之冷埶。 (3) 再者，從LNG槽35a供應至冷熱回收流路犯之 15 1270644 LNG，回收蓄熱於冷熱蓄熱器34a之冷熱，並且以第1氮冷 熱利用熱交換器33c過冷卻而送回至LNG槽35a。因此，能 藉由LNG之過冷卻度來控制LNG槽35a内之B0G之產生， 或使LNG槽35a内之B0G液化來降低LNG槽35a之内壓。 因此，不需要廢棄LNG槽35a内之B0G，經濟上極為有利。 氮循環冷卻機構3之冷熱回收流路35，如氮循環冷卻 機構3之示意部分系統說明圖（本發明之形態丨之變形例i) 之圖5所示，能將LNG供應源槽38a内之LNG，以LNG供應 源泵38b供應至LNG槽35a。又，如此氮循環冷卻機構3之 示意部分系統說明圖（本發明之形態〗之變形例2)之圖6所 示，能將流路c之高純度氮氣以氮壓縮機31職，使流路 D之高純度氮氣混入於此，並且，透過預冷器33f、第 利用熱交換器33a供應至循環壓縮機32。又，依循環壓縮 機32之吸取溫度之設計，不-定需要預冷器33f。、 將本發明之形態2之空氣分離裝置，參 卻機構之示意系統說明圖之圖7 '僱衣~ 口 木祝明。又，本發明夕形 恶2之空氣分離裝置之肩料 y 冷卻箱之構成，因與上述::=:=;_過 僅氮循環冷卻機構不相同，故對同一： 且以同一名稱說明其相異點。 寸琥， 本發明之形態2之空氣分 在氮循環流路33之循環… 乳•冷卻機構3, 縮機（升壓機）33g，將藉 衣叹循％輪機壓 第⑽利該交換^ 32_’並且以 益咖冷卻之屋縮氮氣進-步I縮。此 16 1270644 循％輪機壓细機33g，係以該膨脹輪機33b驅動，以此猶環 輪機屢縮機33g塵縮之塵縮氮氣則以第ilng利用熱交換器 33a冷卻後，以膨脹輪機33b來絕熱膨脹。 ^依本貝施形恶2之空氣分離裝置，因僅將循環輪機壓 、:機33g追加於氮循環冷卻機構3之氮循環流路33，故能 ^隻得與域形態1之空氣分離裝置相等之效果。但是，因 猎由將更⑥®之Μ縮氮氣絕熱膨脹，能使氮猶環流路^之 液態氮之生產效率提高，故比上述形態i之空氣分離裝置 之氮循環流路優異。又，藉由將猶環輪機塵縮機33g及膨 脹輪機33b设置至少2台，能更提高氮猶環流路μ之液態 氮之生產效率。 〜 :本發明之形態3之空氣分離裝置，參閱其氮循環冷 卻枝構之示意系統說明圖之圖8來說明。又，本發明之來 空構^分離裝置之原料空氣處理部、冷箱、液態氮過 …之構成，因與上述形態1之空氣分離裝置相同構成， 僅釓循裱冷卻機構不相同，故對同一構件使用同 且以同一名稱說明其相異點。 ^ ’ 本發明之形態3之空氣分離裝置之氮循環冷卻機 在^循環流路33之循環I缩機32連通至膨脹輪機咖 之抓路之間’設置裝配有循環冷〉東機如之分支 該循環冷滚機饥係使用液態氮或冷媒，將以此循環= 機33!冷部之壓縮氮氣與以第1UG利用熱交換哭 I 之厂堅縮氮氣合流後，以膨脹輪機33b使其絕執騰腰3冷卻 依本實施形態3之空氣分離裝置，因僅將分支流路 17 1270644 33h(裝配有循環冷;東機331)追加於氮循環冷卻機構3之知 循環流路T故能獲得與上述形態！之空氣分離裝置相= 之效果。因藉由將循環輪機壓縮機·設置於氮循環 33二減少循環壓縮機32之氮氣流量，故氮循環流路 液態氮之生產效率，比上述形態丨之空氣 環流路優異。 义乳循 ㈣：本發明之形態' 4之空氣分離裝置’參閱其氮循環冷 籌之不意系統說明圖之》9來說明。又，本發明之形 :二之空氣分離裝置之原料空氣處理部、冷箱、液態氮過 成，因與上述形態1之空氣分離裳置相同構成， 虱4 %冷郃機構不相同，故對同一構件使用同一符號， 且以同一名稱說明其相異點。 " 係從二？明之形態4之空氣分離裝置之氮循環流路… 係吻壓縮機32之排出口，透過第跳利用執交換哭 心、膨脹輪機33b、第1氮冷熱利用熱交換器咖、第2 以熱利用熱交換器33d、第2LNG利用熱 1LNG利用埶夺始口口 00 土 °° 弟 …、又換态33a連通於循環壓縮機32之吸入口。 ’將以氮壓縮機31壓縮之流路c之高純度氮氣、與 二,，純度氮氣的混合氣體，供應至氮循環流路33之 機32之吸入口附近。LNG冷熱蓄熱流路34與冷熱 。《•路3 5之路徑係與上述形態丨之情形同樣。 s、:月之形悲、4之空氣分離裝置，未設置預冷器於 I姚Γ令部機構3。又’氮循環流路33係從循環壓縮機32 口，經由第1LNG利用熱交換器33a、膨脹輪機33卜 18 1270644 第氮利用熱交換器咖、第2氮冷熱利用熱交換器 心= 用熱交換器咖、第1LNG利用熱交換器咖， ^此H循環流路33之氮氣則熱交換至lng(氣液）達 除循環I縮機32之吸取溫度係常溫以外，因lng ▽:畜熱流路34與冷熱回收流路35之經路係與上述形態j :〖广同樣’依本發明之形，態4之空氣分離裝置，能獲得 -逑形態、i之空氣分離裝置相等之效果，惟能採用通常 之吊溫循環壓縮機。 主/本^月之开九％ 4之空氣分離裝置之冷熱回收流'路35 月' 如上述般，從LNG槽35a透過LNG泵35b供應之 …係經由弟2LNG利用熱交換器33e、第1LNG利用熱交 ==連通於冷熱f熱器34a。然而，亦能構成例如使其 由第2LNG利用熱交換器33e，來連通於冷熱蓄熱器 34a(例如熱交換UG至_丨⑽。c為止，又亦能構成為使 :僅=由第2LNG利用熱交換器33e之—半，來連通於冷熱 蓄熱2 34a(例如，熱交換LNG至-i3(rc為止。）。 又，在以上之形態，雖說明將本發明之技術思想適用 於工氣刀離4置之情形’即’當能從⑽槽供應之識之 供應量較多時，佶Τ ΜΓ 更LNG之冷熱畜熱，當能從LNG槽供應之 LNG之供應量較少時，使所f熱之冷熱回收而繼續運轉。然 而’本發明之技術思想’不僅能適用於空氣分離裝置，亦 可適用於未具空氣分離裝置之寒冷產生裝置之循環系統。 【圖式簡單說明】 圖1係本發明之形態1之空氣分離裝置的示意系統圖。 19 !27〇644 圖2，係本發明之 沁毖1之空氣分離 理部的示意系統說明圖 離凌置之原料空氣處 圖3，係本發明之 . 乂恶1之空氣分離奘罢七人 鼠過冷卻部之冷箱的 凌置之冷箱與液態 τ系統說明圖 圖4，係本發明之 ^ 形怨1之空氣分龅酤姐 钱構的示意系統說明圖。 x置之氮循環冷卻 圖 卻機構 圖 卻機構 圖 機構的 圖 機構的 圖 機構的 圖 [A 、 於本發明之形熊1 的示意部分夺綠_ 〜 文形例1 刀糸統說明圖。 6,係相關於本發明之形態i之御 的示意部分+铋 文形例2 刀系統說明圖。 7，係本發明之 <办恶2之空氣分 示意系統說明圖。 破置之 8，係本發明之 心彤恶3之空氣分 示意系統說明圖。 刀離裳置之 9，係本發明之 K形悲4之空氣分離 示意系統說明圖。 破置之 1〇 ’係習知例之空氣分離裝 主要元件符號說明】 糸統圖B、C、D、β、f f 流路 原料空氣處理部 之 氮循環冷 之氮循環冷 循環冷卻 氮猶 氮猶 環冷卻 環冷卻 11 吸取過濾器 12 空氣壓縮機 13 冷卻器 H MS吸附器 20 •1270644 15 再生電熱器 16 消音器 2 冷箱 21 主熱交換器 22 低壓精留塔 23 高壓精留塔 24 過冷卻器 25 富含氧之液態空氣 26 主冷凝器 3 氮循環冷卻機構 31 氮壓縮機 32 循環壓縮機 33 氮循環流路 33a第1LNG利用熱交換器 3 3 b膨脹輪機 33c第1氮冷熱利用熱交換器 33d第2氮冷熱利用熱交換器 33e第2LNG利用熱交換器 33f預冷器 33g循環輪機壓縮機 3 3h分支流路 33i循環冷凍機 34 LNG冷熱蓄熱流路 34a冷熱蓄熱器 21 ‘1270644 35 冷熱回收流路 35a LNG 槽 35b LNG 泵 36 NG排出流路 3 7 LNG加温器 38a LNG供應源槽 38b LNG供應源泵 4 液態氮過冷卻箱 41 氣液分離器 42 液態氮過冷卻器 43 液態氮流路 44 流量控制閥 45 液態氮溫度檢測測感器 46 低溫之氮氣 47 液態氮The m of the cold rail, the nitrogen of the .u 33 is cooled by the heat exchanger 33a using the LNG, and the cooling part is flown to the expansion turbine 33b " The first nitrogen cooling heat utilization heat exchanger 33c for supercooling 12 1270644 LNG, the second nitrogen cold heat utilization heat exchanger 33d for liquefying residual nitrogen not branched by the expansion turbine 33b, and the cooling of nitrogen by the cold heat of LNG 2LNG is cycled using the heat exchanger Me. Further, the first LNG uses the heat exchanger (33a) to cool the nitrogen gas sucked into the nitrogen compressor (31) and sucked into the circulation compressor (32). Further, the nitrogen circulation cooling mechanism 3 is provided with an LNG hot and cold heat storage passage, and is connected to the LNG warmer 37 by the LNG tank 35a, the LNG pump 35b, and the cold and hot heat storage unit 34a for storing the heat of the LNG. Further, the nitrogen circulation cooling mechanism 3 is provided with a cold heat recovery flow path 35 through [gutter 35 & pump 35b, second LNG use heat exchanger 33e, first heat exchange cry 33a, cold heat accumulator 34a, i Nitrogen heat and cold use heat exchanger coffee: j LN ^ Cao 35a. Further, from the portion (10) of the cold heat recovery passage 35 which is discharged by the heat exchanger 33a, the discharge passage 36 is communicated to the LNG warmer 37 via the precooler 33. The NG discharge flow path 36 and the LNG hot and cold heat flow path can also be respectively connected to the respective LNG warmers. The LNG warmer 37 may be, for example, a seawater RV (Ren Rack Vaporizer) or a plug of circulating water. In addition, in this case, the pre-cooling device or the second LNG utilizing heat of the pre-cooling device or the second LNG may be used to pre-cool the pre-cooling device through the flow paths C and D. The exchanger coffee, the first ... = profit: heat exchanger, the second nitrogen cold heat heat exchanger is used to integrate or divide each material. Further, examples of the use of the sputum agent for the hot and cold heat heaters include, for example, Zhengyiyuan, Zhengji, ethanol, methylcyclohexanol, and br. 13-1270644 propanol. The portion of the nitrogen gas compressed by the recycle compressor 32 and utilizing the cold portion of the heat exchanger in the first LNG is expanded by the expansion turbine 33b as described above, but the other nitrogen is branched on the way and passed through the second LNG. The heat exchanger is cooled during the flow path β of the second and second nitrogen cold heat heat exchangers 33d, and the liquid nitrogen is fed into the liquid nitrogen supercooling tank 4 shown in Fig. 3 . Inside the liquid nitrogen supercooling tank 4, as shown on the right side of Fig. 3, the gas liquid separator 41 and the liquid nitrogen subcooler 42 are housed. Namely, the liquid nitrogen supplied from the nitrogen circulation cooling mechanism 3 through the second: E is separated into the low-temperature nitrogen gas 46 and the liquid nitrogen 47 by the gas-liquid separation 141. The gas-liquid separator 41: a portion of the knife-off II gas 46 is sent to the low-pressure retenterator tower 22, and the remainder is merged with the nitrogen gas discharged from the expansion turbine 33b through the passage F. On the other hand, the liquid core (4) nitrogen is too cool! ! 42 It is supercooled and used as a liquid nitrogen coat: it is taken out of the system. A portion of the liquid nitrogen 47 is branched near the outlet of the gas-liquid separator 而 and sent to the top of the high-pressure retentate tower 23. Further, the liquid nitrogen flow path 43 is branched from the outlet of the gas-liquid separator 41, and the nitrogen flow path 43 is used to cause the nitrogen gas to be cooled. In the liquid nitrogen flow path 43, the liquid is disposed according to the liquid state. The detection temperature 42 of the nitrogen temperature detection 45 (to detect the liquid nitrogen temperature of the liquid nitrogen product) cools the liquid, thereby enabling the production of nitrogen products that are subcooled to a predetermined temperature range. The nitrogen cycle according to the aspect 1 of the present invention When the cooling_3' can be supplied in the following two types of operation tanks 35a, the supply amount of lng is large, and 14 1270644 is supplied in parallel with the cold portion of the compressed nitrogen using the first and second LNG heat exchangers 33a and 33e. The hot and cold heat storage passage 34 heats the cold heat of the LNG to the cold heat heat accumulator 34a, and vaporizes the LNG after the heat storage by heating the LNG to 37. On the other hand, when the NG can be supplied from the 35 35 35 35 35 When the LNG supply amount is small, the compressed nitrogen gas is cooled by the cold heat of the LNG supplied from the LNG tank 35a through the LNG pump 3讣 to the cold heat recovery flow path 35, and the LNG which partially or completely gasifies itself is heated up. NG merges with the LNG supplied from the L&NG tank 35a through the LNG pump 35b. It becomes a gas-liquid two-phase grip. Further, by flowing the gas-liquid two-phase flow of the LNG into the cold-heat accumulator 34a, the gas-liquid two-phase flow is liquefied to recover the cold heat, and the cold heat is recovered. The heat is returned to the LNG tank 35a by the heat of the hot parent 33c. In this case, although the cold heat of the nitrogen which adiabatically expands, the cold heat of the liquid nitrogen obtained by the nitrogen circulation cooling mechanism 3 can also be utilized. According to the air separation device of the present invention, the following effects can be obtained. (1) Even if the demand for NG disappears and is not sent out, the cycle can be circulated by the LNG t and the cold heat recovery flow 3535. The compressed nitrogen gas discharged from the circulation compressor π is cooled. That is, since the operation of the circulation compressor is not required to be conventionally controlled, the operation rate of the air separation device can be improved without stopping the operation of the NG. (2) In addition, even if the amount of use of LNG varies greatly, it is not necessary to design the air separation unit with the minimum amount of use of LNG, so it can be used to effectively use the cold enthalpy of LNG. (3) Furthermore, from the LNG tank 35a is supplied to the cold heat recovery flow path 15 127 0644 LNG recovers the cold heat stored in the cold heat heat accumulator 34a, and is supercooled by the first nitrogen cold heat heat exchanger 33c and sent back to the LNG tank 35a. Therefore, the LNG tank 35a can be controlled by the degree of supercooling of the LNG. The generation of B0G or the liquefaction of B0G in the LNG tank 35a reduces the internal pressure of the LNG tank 35a. Therefore, it is not necessary to discard the BOG in the LNG tank 35a, which is economically advantageous. The cold heat recovery flow path of the nitrogen circulation cooling mechanism 3 35, as shown in FIG. 5 of the schematic portion of the nitrogen circulation cooling mechanism 3 (deformation example i of the form of the present invention), the LNG in the LNG supply source tank 38a can be supplied to the LNG supply source pump 38b to LNG tank 35a. Further, as shown in Fig. 6 of the schematic system diagram of the nitrogen circulation cooling mechanism 3 (variation 2 of the embodiment of the present invention), the high-purity nitrogen gas of the flow path c can be used as the nitrogen compressor 31 to form a flow path. The high-purity nitrogen gas of D is mixed therein, and is supplied to the recycle compressor 32 through the pre-cooler 33f and the first heat exchanger 33a. Further, depending on the design of the suction temperature of the circulation compressor 32, the precooler 33f is not required. In the air separation device of the second aspect of the present invention, the schematic system of the supporting mechanism is illustrated in Fig. 7 'women's clothing~ mouth wood Zhuming. Moreover, the structure of the shoulder y cooling tank of the air separation device of the present invention is different from the above-mentioned::=:=;_only nitrogen circulation cooling mechanism, so the same: and the same name is used to describe Different points. Inch, the air of the form 2 of the present invention is circulated in the nitrogen circulation flow path 33. The milk/cooling mechanism 3, the reduction machine (booster) 33g, the sigh of the machine is sighed by the machine pressure (10), the exchange ^ 32_ 'And with the benefit of the coffee cooling house, the nitrogen is reduced into a step. The 16 1270644 follows the % turbine press 33g, which is driven by the expansion turbine 33b, and the dust of the dust is reduced by the heat of the heat exchanger 33a, and then the expansion turbine 33b is cooled by the heat exchanger 33a. Come to adiabatic expansion. According to the air separation device of the Benbes type 2, only the circulating turbine pressure is added to the nitrogen circulation flow path 33 of the nitrogen circulation cooling mechanism 3, so that the air separation device of the domain form 1 can be obtained. Equal effect. However, since the hunting is performed by adiabatic expansion of the nitrogen gas of the 6®, the production efficiency of the liquid nitrogen in the nitrogen gas circulation path is improved, and therefore it is superior to the nitrogen circulation flow path of the air separation device of the above aspect i. Further, by providing at least two sets of the Jubilee turbine dust reducer 33g and the expansion turbine 33b, the production efficiency of the liquid nitrogen of the nitrogen helium circulation path μ can be further improved. ~: The air separation apparatus of the third aspect of the present invention will be described with reference to Fig. 8 of a schematic system diagram of the nitrogen circulation cooling branch. Further, the configuration of the raw material air treatment unit, the cold box, and the liquid nitrogen in the air separation device of the present invention is the same as that of the air separation device according to the first aspect, and only the cooling mechanism is different. The same component uses the same name and its difference is described by the same name. ^ 'The nitrogen circulation cooling machine of the air separation device of the third aspect of the present invention is connected between the cycle I of the circulation flow path 33 and the catching circuit of the expansion turbine coffee machine. The circulating cold rolling machine is hunger-supplied with liquid nitrogen or refrigerant, and this cycle = machine 33! The compressed nitrogen in the cold part is merged with the factory-congested nitrogen gas which is heat-exchanged with the first UG, and is expanded by the expansion machine 33b. According to the air separation device of the third embodiment, only the branch flow path 17 1270644 33h (equipped with circulating cooling; East machine 331) is added to the known circulation flow path T of the nitrogen circulation cooling mechanism 3, so that it can be obtained. With the above form! The effect of the air separation unit phase =. Since the flow rate of the nitrogen gas in the circulation compressor 32 is reduced by installing the circulating turbine compressor in the nitrogen cycle 33, the production efficiency of the liquid nitrogen in the nitrogen circulation flow path is superior to that in the above-described form. Breast milk cycle (4): The air separation device of the form '4 of the present invention' is described with reference to the system description chart of the nitrogen cycle cooling. Further, in the form of the present invention, the raw material air treatment unit, the cold box, and the liquid nitrogen of the air separation device of the second embodiment are configured in the same manner as the air separation device of the above-described form 1, and the 虱4% cold heading mechanism is different, so The same component uses the same symbol and its distinct point is described by the same name. " From the second? The nitrogen circulation flow path of the air separation device of the fourth aspect of the invention is the discharge port of the kiss compressor 32, and the crying heart, the expansion turbine 33b, the first nitrogen heat utilization heat exchanger coffee, and the second heat utilization by the first jump use exchange The heat exchanger 33d and the second LNG use the heat 1LNG to communicate with the suction port of the circulation compressor 32 by the intake port 00. The high-purity nitrogen gas of the flow path c compressed by the nitrogen compressor 31 and the mixed gas of the purity nitrogen gas are supplied to the vicinity of the suction port of the machine 32 of the nitrogen circulation flow path 33. LNG hot and cold heat storage flow path 34 and hot and cold. The path of "•路3 5 is the same as that of the above form. s,: the shape of the moon, the air separation device of 4, the pre-cooler is not provided in the I Yao Yao Department. Further, the 'nitrogen circulation flow path 33 is from the circulation compressor 32, passes through the first LNG use heat exchanger 33a, the expansion turbine 33, and the first nitrogen heat exchanger heat exchanger, and the second nitrogen heat recovery heat exchanger core = heat The exchanger coffee, the first LNG uses the heat exchanger coffee, ^ the nitrogen of the H circulation flow path 33 is heat exchanged to 1 ng (gas liquid) up to the suction temperature of the cycle I reduction machine 32, except for the normal temperature, because of the lng ▽: heat flow of the livestock The path of the road 34 and the cold heat recovery flow path 35 is the same as the above-mentioned form j: [the same as the shape of the invention], and the air separation device of the state 4 can obtain the same effect as the air separation device of the 逑-form, i. Can use the usual hanging temperature cycle compressor. In the case of the above, the cold heat recovery flow of the air separation unit is the same as the above, and the LNG pump 35b is supplied from the LNG tank 35a through the heat exchanger 33e and the first LNG. The heat exchange == is connected to the hot and cold heat heater 34a. However, it is also possible to configure, for example, the second LNG use heat exchanger 33e to communicate with the cold and heat accumulator 34a (for example, heat exchange UG to _(10). The half of the heat exchanger 33e is connected to the hot and cold heat storage 2 34a (for example, heat exchange LNG to -i3 (rc). Further, in the above aspect, the technical idea of the present invention is applied to the air knife. In the case of 4 sets, that is, when the supply of the supply from the (10) tank is large, the hot and cold heat of the LNG is more, when the supply of LNG from the LNG tank is small, the shelter is f The hot and cold heat recovery continues to operate. However, the 'technical idea of the present invention' can be applied not only to the air separation device but also to the circulation system of the cold generation device without the air separation device. [Simplified illustration] Fig. 1 BRIEF DESCRIPTION OF THE DRAWINGS Fig. 2 is a schematic system diagram of an air separation mechanism of the first embodiment of the present invention. Is the invention of the invention. Figure 4 is a schematic diagram of the cold box and liquid τ system of the cold box of the human-cooled section of the cooling unit, and is a schematic system diagram of the air-dividing structure of the invention. The cooling diagram is the diagram of the diagram mechanism of the diagram mechanism of the mechanism diagram mechanism [A, the schematic part of the shape bear 1 of the present invention is green _ _ _ _ _ _ _ _ _ _ _ _ _ _ The schematic part of the form of the invention i is in the form of a knife system. The figure 7 is a schematic diagram of the air system of the present invention. The broken part 8 is the heart of the present invention. The air of the evil 3 is shown in the system diagram. The knife is separated from the skirt, which is the schematic diagram of the air separation schematic system of the K-shaped sadness of the present invention. The broken component is the main component symbol of the air separation assembly of the conventional example. Description] 糸 图 B B, C, D, β, ff Flow path raw material air treatment part of the nitrogen cycle cold nitrogen cycle cold cycle cooling nitrogen helium nitrogen ring cooling ring cooling 11 suction filter 12 air compressor 13 cooler H MS Adsorber 20 • 1270644 15 Regenerative Heater 16 Silencer 2 Cold box 21 Main heat exchanger 22 Low pressure retentate tower 23 High pressure retentate tower 24 Subcooler 25 Oxygen-rich liquid air 26 Main condenser 3 Nitrogen circulation cooling mechanism 31 Nitrogen compressor 32 Recirculating compressor 33 Nitrogen circulating flow Road 33a first LNG heat exchanger 3 3 b expansion turbine 33c first nitrogen cold heat utilization heat exchanger 33d second nitrogen cold heat utilization heat exchanger 33e second LNG use heat exchanger 33f precooler 33g circulation turbine compressor 3 3h Branch flow path 33i circulation freezer 34 LNG hot and cold heat storage flow path 34a hot and cold heat accumulator 21 '1270644 35 cold heat recovery flow path 35a LNG tank 35b LNG pump 36 NG discharge flow path 3 7 LNG warmer 38a LNG supply source tank 38b LNG supply source Pump 4 Liquid nitrogen subcooling tank 41 Gas liquid separator 42 Liquid nitrogen subcooler 43 Liquid nitrogen flow path 44 Flow control valve 45 Liquid nitrogen temperature detection sensor 46 Low temperature nitrogen 47 Liquid nitrogen

22twenty two

Claims (1)

1270644 十、申請專利範圍： 1 · 一種空氣分離裝置，係具備： 空氣壓縮機，將取自大氣之原料空氣壓縮至既定壓力； MS吸附器，供淨化空氣壓縮機所壓縮之壓縮空氣； 精留塔，將該MS吸附器所淨化之壓縮空氣，通過主熱 交換器冷卻後，精留分離為氧與氮；及 氮循環冷卻機構，具有氮循環流路，該流路中設有液 化天然氣利用熱交換器（用來將以該精留塔分離且透過該 主熱父換器取出並以循環壓縮機壓縮之壓縮氮氣，藉液化 天然氣之冷熱冷卻）以及膨脹輪機（用來使該循環壓^機所 排出之壓縮氮氣絕熱膨脹），其特徵在於： 在該氮循環冷卻機構設置： 液化天然氣冷熱蓄熱流路，其經由液化天然氣槽、液 :大然氣泵、用以蓄熱液化天然氣之冷熱之冷熱蓄熱器而 通至液化天然氣加溫器；及 冷熱回收流路，其經由液化天然氣槽、液化天然氣泵、 吕亥液化天然氣利用埶夺她口。 …、、态、々熱蓄熱器、利用該氮循環 冷部機構所產生之突、入^ ^ 槽。 < ~的寒冷熱交換器而回至液化天然氣 2.如申請專利範圍笛 固弟1項之空氣分離裝置，其中，在 口亥虱循環流路之循璟厭 膨脹輪機驅動且以下游側配設升厂堅機，俾使以該 上 升。 盾衣壓縮機壓縮的壓縮氮氣之壓力 如申請專利範圍第j 項之空氣分離裝置，其中， 從 23 1270644 "亥氮循壞流路之循環壓縮機連通至該膨脹輪機的流路·之 間’設置裝設有循環冷凍機之分支流路。 4· 一種空氣分離裝置之運轉方法，其特徵在於：當能 攸液化天然氣槽供應充分量之液化天然氣時，與液化天然 氣之冷熱所作用之壓縮氮氣之冷卻並行，使液化天然氣之 冷熱蓄熱於冷熱蓄熱器，蓄熱後之液化天然氣以液化天然 氣加熱器氣化來製造天然氣； 另一方面’當能從液化天然氣槽供應之液化天然氣之 供應量少時，以從液化天然氣槽經由液化天然氣泵供應之 液化天然氣之冷熱來冷卻壓縮氮氣，並使該液化天然氣本 將 伤或全部氣化的該液化天然氣或天然氣， 一 L方；彳之液化天然氣槽經由液化天然氣泵供應之液化天然 氣，使其成為液化天然氣之2相流後，使其流入該冷熱蓄 熱為使2相流之液化天然氣液化來回收冷熱，並且將冷熱 回收後之液化天然氣送回至該液化天然氣槽。 5 ·如申請專利範圍第4項之空氣分離裝置之運轉方 法’其中，在將該冷熱回收後之液化天然氣送回至液化天 然氣槽之前，利用氮循環冷卻機構所產生之寒冷來冷卻。 十一、圖式： 如次頁 241270644 X. Patent application scope: 1 · An air separation device is provided with: an air compressor for compressing air from a raw material of the atmosphere to a predetermined pressure; an MS adsorber for compressing compressed air by a purified air compressor; a tower, the compressed air purified by the MS adsorber is cooled by a main heat exchanger, and is separated into oxygen and nitrogen; and a nitrogen circulation cooling mechanism has a nitrogen circulation flow path, and the flow path is provided with liquefied natural gas. a heat exchanger (for compressing nitrogen gas which is separated by the fine column and taken out through the main heat master and compressed by a recycle compressor, and cooled by liquefied natural gas) and an expansion turbine (for circulating the pressure) The compressed nitrogen adiabatic expansion discharged by the machine is characterized in that: the nitrogen circulation cooling mechanism is provided: a liquefied natural gas cold heat storage flow path, which passes through a liquefied natural gas tank, a liquid: a natural gas pump, and a cold heat of heat storage for liquefied natural gas a heat accumulator leads to a liquefied natural gas warmer; and a cold heat recovery flow path through a liquefied natural gas tank, a liquefied natural gas pump, Hai liquefied natural gas utilization shame won her mouth. ..., state, hot accumulator, using the nitrogen circulation mechanism generated by the cold section mechanism, into the ^ ^ trough. < ~ cold heat exchanger and return to liquefied natural gas 2. According to the patent application scope, the air separation device of the Descartes 1 item, in which the turbulent venting engine is driven by the circumstance of the loop circulation flow path and is equipped with the downstream side Set up a factory to strengthen the machine, so that the increase. The pressure of the compressed nitrogen compressed by the shield garment compressor is as in the air separation device of the scope of claim j, wherein the flow compressor from the 23 1270644 "sea nitrogen circulation flow path is connected to the flow path of the expansion turbine. 'Set up a branch flow path with a recirculating freezer. 4. A method for operating an air separation device, characterized in that, when a liquefied natural gas tank can supply a sufficient amount of liquefied natural gas, in parallel with the cooling of the compressed nitrogen gas by the cold heat of the liquefied natural gas, the cold heat of the liquefied natural gas is stored in the hot and cold heat. The heat accumulator, the heat-accumulated LNG is gasified by LNG heaters to produce natural gas; on the other hand, when the supply of LNG from the LNG tank is small, it is supplied from the LNG tank via the LNG pump. The cold heat of the liquefied natural gas is used to cool the compressed nitrogen gas, and the liquefied natural gas or the natural gas that is to be completely or gasified by the liquefied natural gas, one L square; the liquefied natural gas tank of the liquefied natural gas tank is liquefied by the liquefied natural gas pump After the two-phase flow of the natural gas, it flows into the cold heat storage to liquefy the liquefied natural gas of the two-phase flow to recover the cold heat, and returns the liquefied natural gas recovered by the cold heat to the liquefied natural gas tank. 5. The method of operating an air separation unit according to claim 4, wherein the liquefied natural gas after the cold heat recovery is returned to the liquefied natural gas tank for cooling by the cold generated by the nitrogen circulation cooling mechanism. XI. Schema: as the next page 24
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Cited By (1)

* Cited by examiner, † Cited by third party
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* Cited by examiner, † Cited by third party
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US7552599B2 (en) 2006-04-05 2009-06-30 Air Products And Chemicals, Inc. Air separation process utilizing refrigeration extracted from LNG for production of liquid oxygen
US8028724B2 (en) 2007-02-12 2011-10-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and unloading of LNG from the tank
US20090199591A1 (en) 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
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