TW483869B - Multiple column nitrogen generators with oxygen coproduction - Google Patents

Multiple column nitrogen generators with oxygen coproduction Download PDF

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Publication number
TW483869B
TW483869B TW088108788A TW88108788A TW483869B TW 483869 B TW483869 B TW 483869B TW 088108788 A TW088108788 A TW 088108788A TW 88108788 A TW88108788 A TW 88108788A TW 483869 B TW483869 B TW 483869B
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Taiwan
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oxygen
column
low
tower
stream
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TW088108788A
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English (en)
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Zbigniew Tadeusz Fidkowski
Donn Michael Herron
Jeffrey Alan Hopkins
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Air Prod & Chem
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • 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
    • 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
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04442—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 at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/90—Triple column

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

Description

483869 五、發明說明（1) 發明背景 本發明涉及在高 回收率高，一般是高 明顯低於1 0 0 %，一般 業應用中，也就是在 時需要少量的氧。當 從空氣進給（從一完 是很不經濟的。因此 具有高的氮回收率和 在製氮的已有技 同時共同產少量氧的 氮發生器可以由 明的改進涉及由兩個 在一雙塔的氮發 餾塔，或者可以使其 應用，不包括再沸器 美國專利4，6 0 4， 該塔帶有對主塔產生 美國專利4，8 4 8， 精德器的氮發生器循 合在一起，它將富氧 體和具有類似於空氣 流被溫熱、壓縮並循 美國專利4，2 2 2，
壓下生產氮和氧的低溫方法，其中氮 於7 0 %，優選高於8 5 %，而氧回收率則 是低於70 %，優選低於55%。在某些工 電子和石油化學工業中，需要氮，有 生產的氧超過需要而又沒有市場時， 全回收設備中）中完全分離氮和氧將 ，就需要一有效的空氣分離設備，即 較低的氧回收率的設備。 術中有幾種方法，但是很少有涉及到 方法。 一個、兩個或多個蒸餾塔組成。本發 或多個塔組成的氮發生器。 生器中，每個塔可以是標準尺寸的分 減小為含有少至一個分顧級（如果能 或冷凝器）的較小分餾器。 11 7使人得知一循環由單一塔組成， 新進料（不同成分）的預分餾器。 9 9 6和4，9 2 7，4 4 1各使人得知一具有後 環。該後分餾器與精餾塔的塔頂熱結 的塔底液體分離成為甚至更富氧的流 成分的汽流。隨後，這種π合成空氣π 環回到精餾塔中。 7 5 6使人得知一傳統的製氮雙塔程序
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第6頁 483869 五、發明說明（2) 循環。在該傳統的雙塔循環中，第一塔（高壓塔）的目的 是將進給空氣分離為塔頂蒸氣氮和富氧液體，及隨後要在 弟一塔（一般在較低的壓力下操作）内對富氧液體加工來 進一步回收氮。 英國專利1，215, 377和美國專利4, 453 ,957、 4，439, 220、4, 617, 036、5, 0 0 6, 139 和 5, 098, 457 使人得知
雙塔氮發生器的各種其它的實施例。在這些專利中公開一 些概念在塔的熱結合措施上有了變化，比如在再沸器/冷 凝器中使用了不同的介質，以及在塔中使用了中間或侧再 /弗器寺。其它的不同是在向設備提供冷來的措施上，比如 用不同介質的膨脹。 美國專利4，7 1 7，4 1 0使人得知另一雙塔氮發生器的程 序流程圖。在此公開的發生器中，通過將液氮從低壓塔泵 回到高壓塔’靠犧牲低壓氮的回收，使高壓氮產物的回收 增加。 美國專利5,069， 699 、 5,402,647和5， 697，229 ，以及 I洲專利0 7 0 1 〇 9 9各公開了包括多於兩個塔的氮發生器流 程圖。附加的塔或塔段被用來進一步增加氮產物的回收和 /或壓力’或者用來提供超高純的氮產物。 溫方法用於生產中 该方法是一全回收 氮來實現比上述參
美國專利5，1 2 9，9 3 2使人得知一低 左氮同日守對氧和氮有高回收率。然而， 的循環。通過膨脹一部份來自高壓塔的 考已有技術更高的氮壓力。 美國專利5,0 4 9, 1 7 3使人得知由任何低溫空氣分離設
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483869 五、發明說明（3) 備製造超高 中進 高於 流0 純氧的原理。具體說來，改進之處包括從其中 一個精餾塔當中取出含氧但無重雜質的物流，在一分餾器 一步汽提該物流的輕雜質，得到超高純的氧。通過從 含重雜質的進料位置處抽出物流而得到無重雜質的物 美國專利4，4 4 8，5 9 5 使人得知一雙塔空氣分離方法的 應用，其中由一部份進給空氣（π分裂塔”）提供低壓塔的 蒸出，得到氮，和任選地得到一些氧。全部氧產物都是從 低壓塔隨著至少一些氮產物產生。氧產物是從低壓塔底或 接近塔底處作為液體抽出，然後在該塔的塔頂被汽化。如 果氧產物的純度高於9 7 %，該專利教導，該產物可以從低 壓塔的塔底抽出。任何過剩的氧可以從低壓塔在廢物流中 抽出。該廢物流還含有氮，這就明顯地降低來自該塔的氮 回收量。該專利發明的改進本身顯示，在高壓下操作低壓 塔，以高壓提供氮產物。因此，廢物流含有過剩的壓力 能，而且使其膨脹為設備提供必要的冷凍。如果由其它裝 置（比如液化器）來提供冷凍，廢物流膨脹器就不再是必 需的而可以除去。 單塔氮發生器與本發明的方法無關，因為它們不能提 供氮的高度回收。然而，為了對背景技術提供更完整的評 論，提供這些專利來公開一些單塔氮發生器循環。 美國專利4，5 6 0，3 9 7和4，7 8 3，2 1 0各使人得知使用單塔 氮發生器共同產氧的方法流程圖。 美國專利4，5 6 0，3 9 7公開一種生產高壓氮以及超高純
第8頁 483869 五、發明說明（4) 氧的方法，在該方法中，使用了兩塔循環，其中第一高壓 塔用來產氮，而氧產物則從第二低壓塔在高於儲液罐的某 一部位取出，以避免重雜質。 美國專利4，7 8 3，2 1 0公開一單塔氮發生器，其中來自 氮發生器底的富氧液體在氮發生器頂的再沸器/冷凝器中 被部份沸騰，造成廢汽物流和第二個富氧液體，最後在一 附加塔中將其純化。 發明要 該方 的回 和一 理除 系統 頂蒸 物流 壓塔 物流 分； 塔的 蒸氣 份進 本發明是對氮發生器的改進，除了主產物氮以外，使 法有效地以低回收率’一般是小於7 0 %，優選小於5 5 % 收率共同產氧。在氮發生器方法中，在具有一高壓塔 低壓塔的蒸餾系統中蒸餾空氣。將進料空氣壓縮、處 去水和二氧化碳、冷卻至接近其露點，並送入蒸餾塔 的高壓塔中。從該蒸餾塔系統的至少一個塔中取出塔 氣物流，得到氮產物。從低壓塔中取出至少一種富氧 。改進的特徵在於：（a )從低壓塔在處於或低於低 進料某一位置處取出富氧物流；（b )將取出的富氧 送入到一補充蒸餾塔中，分離為氧塔底液和廢塔頂餾 (c )為補充蒸餾塔提供蒸出，以及（d )從補充蒸餾 塔底取出氧物流（蒸氣或液體）作為氧產物。 按本發明的方法，可以通過冷凝一部份來自高壓塔的 物流、冷凝一部份來自低壓塔的蒸氣物流、冷凝一部 給空氣或顯冷至少一部份從蒸餾塔系統取出的富氧液
第9頁 483869 五、發明說明（5) 體，來提供補充蒸餾塔的蒸出。 按本發明的方法，可以通過在分離區附近，將一部份 進入該分離區部份的液體或蒸氣進行旁路，來控制補充蒸 餾塔分離區内液體與蒸氣流量的比值。 按本發明的方法，可以通過從低壓蒸餾塔中膨脹富氧 蒸氣、通過從補充蒸餾塔中膨脹廢塔頂餾分或通過至少一 部份壓縮的進料空氣的膨脹來提供程序冷凍。 在本方法中，共同產的氧可以含有大約85%至大約99. 9 9 %的氧。一般說來，這個範圍將在9 5至9 9 . 7%之間。在本 發明的該優選實施例中，加入到補充蒸餾塔的富氧進料從 低壓塔以液體取出。在該最優選的實施例中，加入到補充 蒸餾塔的富氧進料從低壓塔的塔底取出。 圖示之簡單說明 從圖1至5均為本發明方法的幾個實施例示意圖。 圖6是背景技術方法的示意圖。 圖7至1 1均為說明本發明幾個其它實施的示意圖。 下面將參考幾個特定的實施例，詳細地說明在上面綜 述中描述的本發明。在下面的說明中，術語”富氧液體π是 指一液體的含氧量大於空氣中的含氧量。 發明之詳細說明 圖1上示意性地示有本發明的一個可能的實施例。冷 卻的進給空氣1 0 1進入高壓塔1 0 3，在那裡將其分離為塔頂
第10頁 483869 五、發明說明（6) 氮蒸氣1 0 5和第一富氧液體1 〇 7。管路1 0 9中的一部份塔頂 氮蒸氣在再沸器/冷凝器11 1中被液化。管路11 3中的第二 個部份塔頂氮蒸氣在補充再沸器/冷凝器中被液化。可任 選的是管路117中的第三部份塔頂氮蒸氣可以作為高壓氮 產物被取出。液化的氮1 3 5給低壓塔1 1 9提供回流。第一富 氧液體1 0 7在低壓塔1 1 9中進一步被分離為低壓氮蒸氣1 2 1 和第二富氧液體123。經過閥12 5使第二富氧液體降壓，管 路1 2 7中得到的流體被送入一補充蒸館塔，即汽提塔1 2 9 中，在那裡該流體進一步被分離，產生氧產物丨3 1 (作為 液體或蒸氣取出）和廢物流1 3 3。因為氧產物1 3 1比第二富 氧液體1 2 3的氧含量高，所以對於圖1的實施例，汽提塔 1 2 9中的壓力必須低於低壓塔1 1 9中的壓力。補充塔或汽提 塔1 29包括具有再沸器/冷凝器1 1 5 (它可以坐落在儲液槽 殼體内或塔外，但是由液體和蒸氣管路與儲液槽連通）的 儲液槽和由蒸餾塔盤、結構填料或任何其它適當的質傳接 觸器件組成的質傳區1 3 7。 - t 優選使用從低壓蒸餾塔1 1 9的塔底取出的第二富氧液 體1 2 3作為塔1 2 9的進料。然而應該理解，補充蒸餾塔丨2 9 的進料可以是任何從低壓塔由某一低於引進物料部位取出 的含氧流體（在該實施例中是物流1 〇 7 )。而且，雖然在 圖1上未示出’有可能（從低壓塔中）取出第三股富氧物 流。比如可以選擇第三股富氧物流作為蒸氣，以及最終膨 脹所述物流以為程序提供冷束。 對於任何給定的空氣分離設備，對氧的需求會隨時間
第11頁 483869 五、發明說明（7) 而變化。可月匕影 |Α> *1 9 Q rtr V* jUlL γ 1 影響氧產物131的純，。為u體=量比，最終 ^ ^ -¾ ^ ^ ^ ^ 飞其任思邛伤挺供一帶有流量控制閥的 液體或条氣旁路。圖9 + #杳_ > 玖。抟個套改，P =2中有該貫也例具有這樣的蒸氣旁 ° P管路2 4 1帶有流量控制閥2 4 3，它從拔 129的儲液槽通往廢物流133。 匕伙塔 #八m ” 一個實施例是可能的，其中使用不同的加 ”、、”貝為補充塔提供蒸出。圖3示有這個實施例。該循環 的結構和前面的蒸餾塔系統不同之處是，補充汽提塔329 通過再沸器/冷凝器315與低壓塔319熱結合在一起。在這 一實施例中，低壓塔3 1 9内的壓力必須足夠高，使得在該 塔塔頂的溫度足以使在再沸器/冷凝器内的氧沸騰。 圖4中示有本發明的另一實施例。進給空氣1〇1在高壓 塔1 03内被分離為塔頂氮蒸氣1 0 5和第一富氧液體i 〇 7。管 路1 0 9中的一部份塔頂氮蒸氣在再沸器/冷凝器4 11中被冷 凝，並作為回流液返回到高壓塔1 〇 3中。另一部份塔頂氮 蒸氣在管路117中作為高壓氮產物被取出。通過一 jt閥使 第一富氧液體1 07減壓，並被送入小汽提塔445中，在那裡 將其分離為兩股不同組成的蒸氣物流，即管路4 4 7和4 4 9。 通過在再沸器/冷凝器41 1中冷凝氮1 09對塔445提供蒸出。 兩股蒸氣流4 4 7和4 4 9在兩個不同的部位被送入低壓塔4 1 9 中’並在這裡被分離為塔頂氮蒸氣4 5 1和第二富氧液體 1 2 3。管路4 5 3中的一部份塔頂氮蒸氣在再沸器/冷凝器3 1 5 中被冷凝，並作為回流液返回低壓塔419中。管路121中的
第12頁 483869 五、發明說明（8) f 一部份塔頂氮蒸氣作為低壓氮產物被取出。補充塔3 2 9 ，助於再沸器/冷凝器315與低壓塔熱結合在一起。第二富 =液體123經過一】了閥被減壓，並被送入蒸餾塔329中，在 裡將其分離為氧產物3 3 1和廢物流3 3 3。 沾漱f 1 — 4、中的實施例指出’使用來自高壓塔頂的冷凝氮 右杈:丄ί者使用來自低壓塔頂的冷凝氮的潛熱可以為補 冼二叮Γ洛出。對加熱流體的這一特定選擇不是必須的， 拔裎1^，用任何可以得到和適當的程序物流來為氧汽提 ‘ +二ΐ a i比如一部份進給空氣流、從低於高壓塔頂處 一舍二ί ί物流、從低於低壓塔頂處取出的蒸氣物流、第 :氧、、體1 0 7的顯熱等。還應該理解，冷凝的全 伤氮可以從低於可用塔塔頂的位置處取出。 離获Ϊ 5沾中二有曰本發明的另—可能的實施例。這-空氣分 #μ 、☆ ί是以較高的回收率產生蒸氣和液氮，同時以 二、夜f回、產生少量液氧。對於此實施例，為了產生低 液化器結合在-起。然而-般說 合（ϋ J f液化，，比如氮液化器、空氣液化器、混 i在ϋ 口：ί由f化器、含有一個或幾個膨脹透平的液化 态在延一循％中都可以使用。 中J1 ^ 5中/ ^^路5〇1供應進給空氣，使其在主壓縮機503 :f上ίΛ 05中被外面的冷卻流體冷卻，最好在 入到主換孰器511Ϊ ί和二氧化碳，通過管路50 9將其引 ^ ^ 在那裡將其冷卻至低溫的溫度，並 輕由官路513被送入高壓蒸餘塔515中。根據程序規程不
483869 五、發明說明（9) =，高壓塔可以在大約50至大約25 〇磅/平方英 3氣：？？65至150磅/平方英忖面積範圍的壓力下操作。 在局壓塔内被分離產生塔頂氮蒸氣517和第一富 5 2中;J ί 5 2 1人的一部份塔頂氣蒸氣在再沸器/冷凝ί 器/ ί ί ί: Λ 5 *的第二個部份塔頂氮蒸氣在再彿 返回到高壓塔515中’❿管路531中的第二個部份 器521中過冷，經過間5 33減壓，再經管路5 :::送入低壓塔53 7。可以任選地取出管路539中的第 J產物⑷排出。第一富氧液體519在換熱器二：以 f，經過閥543減壓，並經由管路5 4 5被送入低壓塔537 在那裡對其進一步分離為低壓氮蒸氣和第二舍 。低壓塔可以在25至1〇〇磅/平方英忖面積“， 優5和50磅/平方英吋面積之間的壓力下操作。低壓 547在換熱器521和511中被溫熱，並被分成兩股物流：產 物物流551和液化進給物流5 53。可以任選地將物流541中 的全部或一部份高壓氮產物送到氮液化器5 5 5中。一部份 在液化器555中液化的氮在管路557中作為產物被取出，而 =一部份則在管路5 5 9中，用泵561通過管路56 3抽到低壓 塔5 37，作為補充的回流液。第二富氧液體549經過閥 5曰65減壓^，在管路5 6 7中得到的流體在補充塔5 6 9中被蒸餾 提供液氧產物5 7 1和廢物流5 7 3。廢物流5 7 3在換熱器5 ^ i曰和 51 1中被溫熱，經由管路57 5離開該系統。補充塔56\可以
483869 五、發明說明（10) 在接近大氣壓的壓力和更高的壓力下操作，優選範圍是 15-30磅/平方英吋面積。 如果不使用液體冷凍’則可以使用某些形式的膨脹冷 凍。對於圖5中的實施例，人們可以選擇在高壓下操作塔T 5 6 9 ’並且使廢物流5 7 3膨脹。另外也可以選擇膨脹一部份 進給空氣，優選膨脹到低壓塔5 3 7的壓力。最後，可以°選刀 擇從低壓塔中取出富氧蒸氣，並使之膨脹。 ^ 為了顯示本發明的效果，對在圖5中所示的實施例進 行了模擬，計算出其功率消耗，與圖6中所示的具有氮液 化器的傳統雙塔循環進行比較。進行比較時假設每天生產 1500短嘲的含氣不高於5 口口^^的氮產物，並將其後壓縮至 1 5 0碌/平方英吋面積。除了上述氮以外，每天還以純度 9曰9 . 5%生產1 6 5短噸液氧。如圖5所示的本發明的功率消耗 是1 〇 · 2兆瓦。圖6所示的傳統雙塔循環的功率消耗（那裡 排出任何過剩的氧）是1 1 · 4兆瓦。正如從上所述可知，本 發明方是一種更高效的方法。 本發明的其他實施例都是可能的。圖7說明如何可使 了部份進給空氣（物流7 1 3 )在再沸器/冷凝器11 5中冷凝， ^ f補充塔1 2 9提供蒸出。另一方案如圖8所示可使第一富 9W4〇7㊁2彿器1 1 5中顯冷，以對補充塔提供蒸出。圖 蒸餾塔取出Λ程序提供冷；東的不同措施。在圖9中從低壓 ° 、田氧蒸氣作為物流9 2 3並在渦輪9 2 5中膨脹以對 二4 一二5冷；東。在圖10中可使來自補充塔、物流133的 °頂洛乳在渴輪1 035中膨脹以提供冷凍。最後在圖η中使
第15頁 483869 五、發明說明（π) 一部份進給空氣（物流1 1 1 3 )在渦輪1 1 1 5中膨脹，然後將其 引入低壓塔内。 參考了其幾個特定的實施例說明了本發明。這些實施 例不應看作是對本發明的限制。應按照如下的申請專利範 圍來確定本發明的範圍。
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Claims (1)

  1. j〇Oy 六、申請專利範圍 ^88Γ
    日___i3ri 壓塔的蒗和種^条餾空氣;的低溫方法，用在具有高壓塔和低 處理除去=合糸統中生產氮產物，其中將進給空氣壓縮、 :系：的7高ί 2化碳、冷卻至接近其露·點’並送入蒸餾 出i sϊ ί物流，生產氮產物，以及其中從低壓塔中取 物流是液流二該方法的特徵在於：“）該富氧 的；（b)w疋攸低壓塔一低於低壓塔進給位置處取出 〇 :取出的液體富氧物流送入一補# Y ^ ϋ Μ Tf :充為-氧塔底液和-廢塔以 蒸氣物流；i氧ί:: 乂)r從補充蒸館塔的塔底取出氧 壓力下操作該補充。e)在—壓力低於低壓塔的 2·如申請專利範圍第1項的方法， 份來自高壓塔的基^ _ 、中通過冷凝一部 …、孔物々丨L k供補充蒸餾塔的蒸出。 3 ·如申請專利範圍第1項的方法，复+ 份來自低壓塔的蒸氣物流提供補充蒸餘塔冷凝-部 4 · 士申叫專利範圍第1項的方法，复 份進給空氣提供補充蒸餾塔的蒸出。”中通過冷凝一部 5·如申請專利範圍第1項的方法，苴 一部份從蒸館塔系…统中取出的s氧;、夜體接通過顯冷至>、 蒸出。 &供補充蒸德塔的
    2002.03.15.018 483869 _案號88108788_年月日__ 六、申請專利範圍 6. 如申請專利範圍第1項的方法，其中補充蒸餾塔包 括至少一個分離區，在那裡蒸氣和液體逆向流動接觸，而 且其中通過在分離區周圍將一部份要進入這部份分離區的 液體或蒸氣加旁路來控制分離區内液體流量與蒸氣流量的 比例。
    7. 如申請專利範圍第1項的方法，其中從低壓蒸餾塔 取出富氧蒸氣，並且使其膨脹以提供自身方法冷凍。 8. 如申請專利範圍第1項的方法，其中從補充蒸餾塔 取出廢塔頂餾分，並使其膨脹以提供自身方法冷凍。 9. 如申請專利範圍第1項的方法，其中通過膨脹至少 一部份壓縮的進給空氣來提供自身方法冷凍。 10. 如申請專利範圍第1項的方法，其中進給空氣中 少於7 0 %的氧被回收在氧產物中。 11. 如申請專利範圍第1項的方法，其中進給空氣中 少於55%的氧被回收在氧產物中。 12.如申請專利範圍第1項的方法，其中氧產物的氧 濃度在85和99. 9 9%氧之間。
    \\Adm-host\20010610\pl900\airl946,\mend01.ptc 第18頁 2002.03.15.019 483869 _ 案號88108788_年月日__ 六、申請專利範圍 13.如申請專利範圍第1項的方法，其中氧產物的氧 濃度在95和99. 7%氧之間。 1 4.如申請專利範圍第1項的方法，其中富氧物流是 從低壓塔的塔底取出。
    \\Adm-host\20010610\pl900\airl946Amend01.ptc 第 19 頁 2002. 03. 15. 020
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