CN1091868C - 带釜液塔的低温精馏*** - Google Patents

带釜液塔的低温精馏*** Download PDF

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CN1091868C
CN1091868C CN97114081A CN97114081A CN1091868C CN 1091868 C CN1091868 C CN 1091868C CN 97114081 A CN97114081 A CN 97114081A CN 97114081 A CN97114081 A CN 97114081A CN 1091868 C CN1091868 C CN 1091868C
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N·M·普罗瑟
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    • 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
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    • 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
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    • 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
    • F25J3/04448—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 an intermediate pressure column
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    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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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
    • 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
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Abstract

用于生产氧和氮的低温精馏***，使用了一釜液塔，它处理来自高压塔的富氧釜液以及被取自高压塔顶部下方的流体所再沸。

Description

带釜液塔的低温精馏***
本发明一般地涉及进料空气的低温精馏，更具体地涉及进料空气的低温精馏以生产氧和氮。
进料空气的低温精馏一般在双塔***中进行，其中在高压塔进行初始分离而在低压塔内进行最终分离。在低层塔中在略大于环境压力下制得各种产品。
在某些情况下，在加压时需要氧和氮产品中的一个或两个。特别是在加压下将氮从***中导出时，将没有足够的回流以有效地操作各塔。
因此本发明的一个目的是提供用于生产氧和氮的低温精馏***，即使在加压下生产各产品的一个或两个时，都可有效地进行操作。
本领域技术人员在阅读了本公开后，本发明所完成的上述及其它目的将显而易见。其一方面是：
生产氧和氮的低温精馏方法，包含：
(A)将进料空气送入高压塔，并在高压塔内通过低温精馏将进料空气分离成富氧釜液和富氮顶部流体；
(B)将富氧釜液送入釜液塔，并在釜液塔内通过低温精馏产生中间蒸气和中间液体；
(C)将自高压塔顶部下方取出的蒸气流与中间液体进行间接热交换以产生高压液体并将高压液体送入高压塔中；
(D)将来自釜液塔中的液体送入低压塔中，并在低压塔内通过低温精馏生成富氮流体和富氧流体；和
(E)将至少一些富氧流体作为产品氧回收，以及将至少一些中间蒸气、富氮顶部流体和富氮流体中的至少一个作为产品氮回收。
本发明的另一方面是：
生产氧和氮的低温精馏设备，包括：
(A)第一塔、第二塔以及将进料空气送入第一塔的装置；
(B)具有底部再沸器的釜液塔以及将来自第一塔下部的流体送入釜液塔的装置；
(C)将来自第一塔顶部下方的流体送入釜液塔底部再沸器的装置以及将来自釜液塔底部再沸器的流体送入第一塔的装置；
(D)将来自釜液塔的流体送入第二塔的装置；和
(E)将来自第二塔下部的流体回收的装置以及将来自第一塔、第二塔和釜液塔中至少一个上部的液体回收的装置。
此处所用的术语“塔盘”意指一接触段，它不必是一平衡段，也可指其它接触设备如分离能力相当于一个塔盘的填料。
此处所用的术语“平衡段”意指气-液接触段，其中离开该段的气体和液体处于传质平衡，如100％效率的塔盘或相当于一理论塔板(HETP)的填料单元高度。
此处所用的术语“进料空气”意指主要包含氧和氮的混合物如环境空气。
此处所用的术语“塔”意指蒸馏或分馏塔或区，即接触塔或区，其中液相和气相逆液接触以实现流体混合物的分离，如通过气相和液相在置于塔内的一系列垂直放置的塔盘或塔板和/或填料单元如结构或无规填料上接触。对蒸馏塔进一步的讨论，参见《化学工程师手册》第5版，R.H.Perry和C.H.Chilton编，Mc Graw-Hill Book Company出版，纽约，第13段，“连续蒸馏法”。所用的术语“双塔”意指其上部与一低压塔下部处于热交换关系的高压塔。对双塔的进一步讨论可参见Ruheman的“气体分离”，牛津大学出版社，1949，第VII章，工业空气分离。
气液接触分离法基于各组分蒸气压的不同。高蒸气压(或易挥发或低沸点)组分易于浓缩于气相而低蒸气压(或难挥发或高沸点)组分易于浓缩于液相。部分冷凝是蒸气混合物的冷却可用来在气相中浓缩挥发组分而难挥发组分在液相中的分离方法。精馏或连续蒸馏是结合通过气相和液相的逆流处理所获得的连续部分蒸发和冷凝的分离方法。气相和液相的逆流接触基本上是绝热的并可包括相互间的积分(阶段的)或微分(连续的)接触。利用精馏的原理来分离混合物的分离方法设备常可互换地称为精馏塔、蒸馏塔或分馏塔。低温精馏是一种在至少部分在温度等于或低于150度开尔文(K)下进行的精馏方法。
此处所用的术语“间接热交换”意指各流体之间在没有任何物理接触或混合的情况下将两种流体导入热交换关系。
此处所用的术语“再沸器”意指比塔液体中产生塔上流蒸气的热交换装置。
此处所用的术语“汽轮膨胀”和“汽轮骤冷器”分别意指高压气流通过一汽轮机以降低气体的压力和温度藉以产生制冷作用的方法和设备。
所用的术语“上部”和“下部”意指分别位于塔中点以上和以下的塔的各段。
此处所用术语“底部”当涉及一塔时，意指低于塔传质内件即塔盘或填料的塔段。
此处所用的术语“底部再沸器”意指从塔底沸腾液体的再沸器。底部再沸器可位于塔内或塔外。
此处所用的术语“中间再沸器”意指从塔底上方沸腾液体的再沸器。“中间再沸器”可位于塔内或塔外。
此处所用术语“顶部”当涉及一塔时，意指在塔传质内件即塔盘或填料之上的塔段。
此处所用的术语“釜液塔”意指处理取自另一塔的下部、优选为底部的流体的塔。
仅有的图为本发明一优选实施方案的示意图。
本发明使用一釜液塔以产生附加的液体回流从而可以有效地生产高压产品。通过取自高压塔下方的流体来驱动该釜液塔。这种流体的氧含量及其温度超过高压塔顶部流体。该较高温度的流体使得釜液塔底部的温度高于低压塔底部的温度。流体较高的温度也使高压流体流动增加，从而导致釜液塔内较高的蒸气上流和液体下流。结果与常规***相比增加了回流液的生成，从而提高了产品回收率和/或增加了平均产品氮压力。
本发明将参照图详细加以描述。现参照图，进料空气30通过压缩机22被压缩至绝对压力一般在448.2-2241 kPa[65-325磅/平方英寸](绝对压)的范围。通过净化器23清除被压缩进料空气32的高沸点杂质如二氧化碳和水蒸气，所得清洁、压缩的进料空气被送入高压塔。示于图中的实施方案是一优选实施方案，其中只有部分清洁、压缩的进料空气被送入高压塔中。再参照图，清洁、压缩的进料空气34被分成三部分：36、38和44。包含进料空气34至少60％(一般为约60％-75.5％)的第一部分36经过主换热器17通过与返回流进行间接热交换而得到冷却。所得进料空气流60被送入在压力一般为413.7-2206kPa[60-320psia]下操作的第一或高压塔中。
当使用第二进料空气部分38时，一般包含流34的约24％-34％。当需要高压氧产品时流用于蒸发受压液体。通过压缩机24流38被压缩至压力一般为517.1kPa-17.24MPa[75-2500psia]、优选861.8kPa-8.963MPa[125-1300psia]，并且通过冷却器25，所得加压流40被冷却至接近环境温度。所得流42通过主换热器17而在其中被冷凝。如图所示，流64中的所得液体被送入至少一个或所有三个用于本发明实践中的塔中(虽然流64的部分流68进入釜液塔是可选的)。第一液体部分70经部分横过换热器16而得到低温冷却，通过阀164并作为流72被送入第二或低压塔12中。塔12是也包括高压塔10的双塔***中的低压塔，并在低于高压塔10的压力下(一般在约110.3-861.8kPa[16-125psia])操作。
流64的剩余部分被送入高压塔10并可选地被送入到压力在高压塔及低压塔之间(一般在约241.3-1586kPa[35-230psia])下操作的釜液塔11中。参照图，液流64的可选部分68送经阀161并进入釜液塔11中，液流64的部分66送经阀160并进入高压塔10中。
当使用第三进料空气部分44时一般包含进料空气流34的约0.5-6％。通过压缩机20流44被压缩至压力一般在689.5-3792kPa[100-550psia]的范围内。所得压缩流46通过冷却器21被冷却至接近环境温度，所得流48通过部分横过主换热器17而得到冷凝。所得流50经汽轮骤冷器19而被汽轮膨胀以产生制冷作用，所得汽轮膨胀流52被送入低压塔12中。通过汽轮骤冷器19产生的能量通过轴26来驱动压缩机20。
高压塔10内被送入该塔的进料空气通过低温精馏被分离成富氧釜液和富氮顶部流体。富氮顶部液体蒸气流110从高压塔10的顶部导出。如图中所示，若需要，流110的部分120通过主换热器17而得到加热，并作为氮浓度一般为至少97％(摩尔)的产品高压氮122而得到回收。若需要，流120的部分可在部分横过主换热器17后被导出，进行汽轮膨胀以产生制冷作用并返回各塔中。
包含富氮顶部流体流110剩余部分的流112被送入低压塔12的底部再沸器13，在其中通过与沸腾的低压塔底部液体进行间接热交换而得到冷凝。所得冷凝富氮顶部液体114作为回流被送入低压塔12和高压塔10中。流114的第一部分94通过部分横过换热器16而得到低温冷却、该部分通过阀166膨长并作为流96被送入低压塔12的上部。流114的第2部分116被送入高压塔10的上部。若需要，液体富氮顶部流体114的部分也可作为回流被送入釜液泵11的上部。
氧含量一般在29-42％(摩尔)的富氧釜液在流80中从高压塔10的下部导出，通过部分横过换热器16而得到低温冷却，通过阀162降低了压力并作为流82被送入釜液塔11中。
在釜液塔11内，进入该塔的进料通过低温精馏被分离成中间蒸气和中间液体。氧浓度一般在38-51％(摩尔)的中间液体在流83中从釜液塔11的下部导出经阀163，然后作为流84被送入低压塔12中。氮浓度至少为97％(摩尔)的中间蒸气作为流100从釜液塔11的上部导出，并进入低压塔12的中间再沸器15中。所得含氮液102被分成流104(作为回流被送入釜液塔11的上部)以及流106(通过部分横过提热器16而被低温冷却)，经阀165膨胀并作为附加回流流108被送入低压塔12的上部。若需要，中间蒸气100的部分可作为氮蒸气产品回收。
通过取自高压塔10顶部下方的高压蒸气流90来驱动釜液塔11。流90的氧浓度超过富氮顶部流体的氧浓度，一般在0.5-8％(摩尔)的范围内。流90取自高压塔10顶部下方的1-15个平衡段、优选4-15个平衡段的位置。若被送入釜液塔底部再沸器的所述流取自上述定义范围内的最适位置的上方，则不能产生所需的增加回流，而若取自该范围内的下方位置，则产品回收率将受到危害。流90被送入釜液塔11的底部再沸器14，在其中通过与釜液塔底部液体进行间接热交换而得到冷凝。所得液流92在与流90从高压塔10被导出的相同位置或其上方被重新送回高压塔10中。
因为流90具有较高的氧浓度因而温度高于再沸低压塔12底部的富氮顶部流体的温度，所以被流90再沸的釜液塔11的底部具有较高的温度，一般比低压塔12底部高0.5-2.0°K。该较高温度使得流90的流量得以增加，导致釜液塔11内较高的蒸气上流和液体下流。这依次增加了从塔11导出的中间蒸气的流动，结果增加了在流108中被送入低压塔12的附加回流的形成。附加回流增加了产品回收率，或增加了富氮顶部流体或中间蒸气流动的能力，或增加了该***压力的能力，使得节省压缩功率。
在低压塔12中通过低温精馏将各种进入该塔的进料分离成富氮流体和富氧流体。氧浓度一般在70-99.5％(摩尔)、优选在80-98(摩尔)范围内的富氧流体作为流130从低压塔12的下部导出并作为产品氧回收。若需要，如图所示，流130的压力可通过泵18被加压至206.8kPa-13.79MPa[30-2000psia]、优选44.7kPa-8.963MPa[50-1300psia]的范围内，然后加压流132通过主换热器17而得到蒸发并作为氧产品的流134回收。
氮浓度一般至少为97％(摩尔)的富氮流体作为流140从低压塔12的上部导出，通过换热器16和主换热器17得到加热，并作为流144从该***中导出。若需要，流144的部分或全部可作为低压氮产品得到回收。若需要，流140的部分可在部分横过主换热器17后被导出，并进行汽轮膨胀以产生制冷作用。然后，所得汽轮膨胀流可经主换热器17，其中制冷作用可通过间接热交换而被送入进入的进料流中。
通过本发明的实践，尤其是在加压下，人们可有效地生产氧和氮产品，而不会遇到缺乏回流的塔的情况。虽然本发明参照本发明的一优选实施方案已做了详细描述，但本领域技术人员将会理解在本 书的精神和范畴内本发明的其它实施方案。例如来自釜液塔的中间蒸气可通过与来自釜液塔的液体而不是与来自低压塔的流体进行间接热交换而得到冷凝。

Claims (6)

1.生产氧(134)和氮(122，144)的低温精馏方法，包括：
(A)将进料空气(60，66)送入高压塔(10)并在高压塔内通过低温精馏将该进料空气分离成富氧釜液(80)和富氮顶部流体(110)；
(B)将富氧釜液(80)送入釜液塔(11)中并在釜液塔内通过低温精馏产生中间蒸气和中间液体；
(C)将取自高压塔(10)顶部下方的蒸气流(90)通过与中间液体进行间接热交换以产生高压液体(92)，并将高压液体送入高压塔内；
(D)从釜液塔(11)的上部导出中间蒸气(100)，将该中间蒸气冷凝，将所得液体(102，108)送入低压塔(12)并在低压塔内通过低温精馏产生富氮流体(140)和富氧流体(130)；和
(E)将至少一些富氧流体(130)作为产品氧(134)回收，以及将至少一些中间蒸气(100)、富氮顶部流体(110)及富氮流体(140)中的至少一个作为产品氮(122，144)回收；
其特征在于，
在步骤(C)中，所述蒸气流(90)从高压塔(10)的顶部下方1-15个平衡段的位置取出，并且所述高压液体(92)从所述蒸气流(90)从高压塔取出的位置或其上方被送入高压塔(10)中。
2.权利要求1的方法，其中中间蒸气(100)从釜液塔(11)的上部导出，冷凝，所得液体(102，104)被送入釜液塔中。
3.权利要求2的方法，其中中间蒸气(100)通过与来自低压塔(12)和釜液塔(11)中至少一个的流体进行间接热交换而得到冷凝。
4.生产氧和氮的低温精馏设备，包括：
(A)高压塔(10)、低压塔(12)以及将进料空气(60，66)送入高压塔的装置；
(B)具有底部再沸器(14)的釜液塔(11)以及将来自高压塔(10)下部的富氧釜液(80)送入釜液塔的装置，
(C)将来自高压塔(10)顶部下方的蒸气(90)送入釜液塔底再沸器(14)的装置，以及将来自釜液塔底部再沸器的高压液体(92)送入高压塔的装置；
(D)将来自釜液塔的流体送入低压塔的装置；和
(E)将来自低压塔(12)下部的富氧流体(130，134)回收的装置，以及将来自高压塔(10)、低压塔(12)和釜液塔(11)中至少一个的上部的产品氮(110，122，140，144)回收的装置；
其特征在于，
所述将来自高压塔(10)顶部下方的蒸气(90)送入釜液塔底再沸器(14)的装置与高压塔在高压塔顶部下方1-15个平衡段的位置相连接，以及所述将来自釜液塔底部再沸器(14)的高压液体(92)送入高压塔(10)的装置与高压塔在蒸气从高压塔被送入釜液塔底部再沸器的位置或其上方相连接。
5.权利要求4的设备，其中还包括将来自釜液塔下部的中间液体(83)送入低压塔(12)中的装置。
6.权利要求4的设备，其中还包括用于低压塔(12)的中间再沸器(15)、将来自釜液塔(11)上部的中间蒸气(100)送入该中间再沸器的装置，以及将来自该中间再沸器的流体(102，108)送入低压塔(12)上部的装置。
CN97114081A 1996-11-07 1997-07-02 带釜液塔的低温精馏*** Expired - Lifetime CN1091868C (zh)

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Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5682764A (en) * 1996-10-25 1997-11-04 Air Products And Chemicals, Inc. Three column cryogenic cycle for the production of impure oxygen and pure nitrogen
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
US5901578A (en) * 1998-05-18 1999-05-11 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler
US6000239A (en) * 1998-07-10 1999-12-14 Praxair Technology, Inc. Cryogenic air separation system with high ratio turboexpansion
US6116052A (en) * 1999-04-09 2000-09-12 Air Liquide Process And Construction Cryogenic air separation process and installation
US6276170B1 (en) 1999-05-25 2001-08-21 Air Liquide Process And Construction Cryogenic distillation system for air separation
US6202441B1 (en) 1999-05-25 2001-03-20 Air Liquide Process And Construction, Inc. Cryogenic distillation system for air separation
US6347534B1 (en) 1999-05-25 2002-02-19 Air Liquide Process And Construction Cryogenic distillation system for air separation
US6196024B1 (en) 1999-05-25 2001-03-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation system for air separation
US6192707B1 (en) 1999-11-12 2001-02-27 Praxair Technology, Inc. Cryogenic system for producing enriched air
US6227005B1 (en) * 2000-03-01 2001-05-08 Air Products And Chemicals, Inc. Process for the production of oxygen and nitrogen
US6286336B1 (en) * 2000-05-03 2001-09-11 Praxair Technology, Inc. Cryogenic air separation system for elevated pressure product
US6460373B1 (en) * 2001-12-04 2002-10-08 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US6536234B1 (en) 2002-02-05 2003-03-25 Praxair Technology, Inc. Three column cryogenic air separation system with dual pressure air feeds
US7114352B2 (en) * 2003-12-24 2006-10-03 Praxair Technology, Inc. Cryogenic air separation system for producing elevated pressure nitrogen
US20070095100A1 (en) * 2005-11-03 2007-05-03 Rankin Peter J Cryogenic air separation process with excess turbine refrigeration
US8286446B2 (en) * 2008-05-07 2012-10-16 Praxair Technology, Inc. Method and apparatus for separating air
US8443625B2 (en) * 2008-08-14 2013-05-21 Praxair Technology, Inc. Krypton and xenon recovery method
US8479535B2 (en) * 2008-09-22 2013-07-09 Praxair Technology, Inc. Method and apparatus for producing high purity oxygen
FR3011916B1 (fr) * 2013-10-15 2015-11-13 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US20240035741A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser Air separation unit and method for cryogenic separation of air using a distillation column system including an intermediate pressure kettle column
US20240035745A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser System and method for cryogenic air separation using four distillation columns including an intermediate pressure column
US11959701B2 (en) 2022-07-28 2024-04-16 Praxair Technology, Inc. Air separation unit and method for production of high purity nitrogen product using a distillation column system with an intermediate pressure kettle column
US20240035744A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser Air separation unit and method for production of nitrogen and argon using a distillation column system with an intermediate pressure kettle column

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2057660B (en) * 1979-05-17 1983-03-16 Union Carbide Corp Process and apparatus for producing low purity oxygen
US4605427A (en) * 1983-03-31 1986-08-12 Erickson Donald C Cryogenic triple-pressure air separation with LP-to-MP latent-heat-exchange
US5231837A (en) * 1991-10-15 1993-08-03 Liquid Air Engineering Corporation Cryogenic distillation process for the production of oxygen and nitrogen
FR2685459B1 (fr) * 1991-12-18 1994-02-11 Air Liquide Procede et installation de production d'oxygene impur.
CN1071444C (zh) * 1992-02-21 2001-09-19 普拉塞尔技术有限公司 生产气体氧的低温空气分离***
US5263327A (en) * 1992-03-26 1993-11-23 Praxair Technology, Inc. High recovery cryogenic rectification system
GB9405071D0 (en) * 1993-07-05 1994-04-27 Boc Group Plc Air separation
US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
US5467602A (en) * 1994-05-10 1995-11-21 Praxair Technology, Inc. Air boiling cryogenic rectification system for producing elevated pressure oxygen
US5440884A (en) * 1994-07-14 1995-08-15 Praxair Technology, Inc. Cryogenic air separation system with liquid air stripping
GB9414939D0 (en) * 1994-07-25 1994-09-14 Boc Group Plc Air separation
US5463871A (en) * 1994-10-04 1995-11-07 Praxair Technology, Inc. Side column cryogenic rectification system for producing lower purity oxygen
US5469710A (en) * 1994-10-26 1995-11-28 Praxair Technology, Inc. Cryogenic rectification system with enhanced argon recovery
GB9425484D0 (en) * 1994-12-16 1995-02-15 Boc Group Plc Air separation
US5546767A (en) * 1995-09-29 1996-08-20 Praxair Technology, Inc. Cryogenic rectification system for producing dual purity oxygen

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