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CN1214444A - 用于生产高压氧的低温精馏系统 - Google Patents

用于生产高压氧的低温精馏系统 Download PDF

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CN1214444A
CN1214444A CN98120912.2A CN98120912A CN1214444A CN 1214444 A CN1214444 A CN 1214444A CN 98120912 A CN98120912 A CN 98120912A CN 1214444 A CN1214444 A CN 1214444A
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CN1123752C (zh
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N·J·林奇
D·P·伯纳奎斯特
S·G·弗赖
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Praxair Technology Inc
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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
    • F25J3/04248—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
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
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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
    • F25J3/04406—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
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Abstract

用于生产高压氧的低温精馏系统,其中使部分进料空气通过与加压过的液氧间接热交换冷凝,然后优选在过冷之后流入双塔系统中的低压塔。

Description

用于生产高压氧的低温精馏系统
技术领域
本发明一般涉及使用双塔系统低温精馏进料空气生产氧，更具体地说，涉及氮或者氩都不从双塔中的低压塔生产的系统。
背景技术
工业上通过低温精馏进料空气大量地生产氧，通常使用众所周知的双塔系统，其中产品氧取自于低压塔。有时要求在压力超过从低压塔取出氧时的压力下生产氧。在这种情况下，要把气体氧压缩至预定的压力。然而，就投资费用来说，通常最好是提高氧的压力，使其能作为液体从低压塔中移出，再使加压过的液体氧蒸发，生产出所要求的高压产品氧气。
典型地，采用这样一种双塔系统时，在低压塔内也能生产出产品氮，并能从该塔中将其回收。此外，经常有一股来自低压塔的流体流入能在其中生产氩的氩侧塔中，然而，有时要求直接或间接来自低压塔的唯一产品是氧，在这样的情况下，不可避免要尽可能有效地操作系统，因为不能利用低压塔产生氮或者氩作产品，以便补偿该系统的投资和操作费用。当要求高压产品氧时，因为这会进一步增加该系统的费用，所以这是一种特殊的情况。
因此，本发明的目的在于提供一种用于生产高压氧的改进的双塔低温精馏系统，其中不从低压塔直接或间接回收其它的产品。
发明概述
基于阅读本说明书，对所属领域的技术人员将明了的上述和其它目的，由本发明予以完成，本发明的一个方面是：
一种生产高压氧的方法，该法包括：
(A)使进料空气的第一部分通入高压塔且使由该高压塔流出的流体通入低压塔；
(B)使进料空气的第二部分冷凝并使所生成的液体进料空气通入低压塔；
(C)在低压塔内通过低温精馏生产液体氧；
(D)提高液体氧的压力以便生产高压液体氧，再通过与冷凝的进料空气第二部分间接热交换来蒸发高压液体氧以便生产高压氧气；和
(E)回收高压氧气。
本发明另一方面是：
用于生产高压氧的设备，该设备包括：
(A)第一塔、第二塔，以及用于使进料空气通入第一塔的装置；
(B)产品锅炉，用于使进料空气通入该产品锅炉的装置，以及用于使来自产品锅炉的进料空气通入第二塔的装置；
(C)用于使来自第一塔的流体通入第二塔的装置；
(D)用于从第二塔的下部排出流体、提高排出的流体压力、以及使被排出流体通入产品锅炉的装置；和
(E)用于从产品锅炉回收高压氧产品的装置。
本文所用术语“液体氧”意指具有至少98％(摩尔)氧浓度的液体。
本文所用术语“进料空气”意指主要含氮、氩和氧的混合物，如环境空气。
本文所用术语“产品锅炉”意指热交换器，其中液体氧被蒸发和进料空气被冷凝。产品锅炉可以是单独的热交换器也可以是低温空气分离装置的初级热交换器的一部分。
本文所用术语“过冷”和“过冷却器”分别指用于冷却一种液体到低于就存在压力而言该液体饱和温度的温度的方法和设备。
本文所用术语“涡轮膨胀”和“涡轮膨胀机”分别指用于高压气体流经过涡轮以降低气体的压力和温度的方法和设备。
本文所用术语“塔”意指蒸馏或分馏塔或区，即，接触塔或区，其中液相和气相逆流接触以便进行流体混合物的分离，例如，通过气相和液相在一系列安装在塔内垂直隔开的塔盘或塔板和/或结构填充元件和/或无规填充元件上接触。为了进一步讨论蒸馏塔可参见化学工程师手册第五版，由R.J.佩里和C.H.奇尔顿编，麦格劳-希尔图书公司，纽约，第13节，连续蒸馏法(Chemical Engineers′Handbook fiftheditioh,edited by R.J.Perry and C.H.Chilton,McGraw-HillBook Company,New York,Section 13,The Continuous DistillationProcess)。术语，双塔用来表示具有与低压塔下端有热交换关系的上端的高压塔。双塔的进一步讨论发表在Ruheman的“气体分离”中，牛津大学出版社，1949,Ⅶ章，工业用空气分离(“The Separationof Gases”,Oxford University Press,1949,Chapter Ⅶ,Commercial Air Separation)。
气液接触分离法取决于各成分蒸气压的差别。高蒸气压(或更易挥发或低沸点)的组分倾向于在蒸气相中浓缩而低蒸发压(或不易挥发或高沸点)的组分倾向于在液相中浓缩。部分冷凝是一种把蒸气混合物的冷却用于浓缩挥发性组分于蒸气相中而由此减少液相中挥发性成分的分离方法。精馏，或连续蒸馏，是一种由逆流处理气液相所得到的连续部分蒸发和冷凝融合起来的分离方法。气液相逆流接触是绝热的且在相间包括积分或微分接触。利用精馏原理去分离混合物的分离方法装置是经常可互换叫做精馏塔、蒸馏塔或分馏塔。低温精馏是至少部分在或低于开氏(K)150度下进行的精馏过程。
本文所用术语“间接热交换”意指使两种流体建立热交换关系但无任何物理接触或流体的相互混合。
本文所用塔的“上部”和“下部”分别指该塔中点以上和以下的那些部分。
本文所用术语塔“顶”意指该塔内部构件，例如塔盘或填料上面塔的部分。
附图的简要描述
图1是本发明低温精馏系统一种最佳实施方案的示意图。
图2是本发明低温精馏系统另一最佳实施方案的示意图。
详细说明
将参照附图对本发明详细进行说明。
现参照图1，已清除高沸点杂质如水蒸气、二氧化碳和碳氢化合物的进料空气60，其压力通常在每平方英寸70-100磅绝对压力(psia)范围内，被分成第一部分61、第二部分67和第三部分63。第一部分61，含有约60-76％的进料空气60，由于流经初级热交换器1而被冷却再使所得到的冷却进料空气第一部分62流入第一或高压塔10。
第二进料空气部分67，含有约20-30％的进料空气60，通过流经压缩机32进一步被压缩至120-500psia范围内的压力。正如在下文将要进一步讨论的，通过与初级热交换器1的产品锅炉部分中的液体氧间接热交换使所生成的高压第二进料空气部分68被冷凝。在图1所说明的本发明实施方案中，产品锅炉是包括热交换通道A和B在内的初级热交换器1的一部分。
来自产品锅炉所生成的液体进料空气69在塔的中间高度处，即塔11顶部的下面流入第二或低压塔11中。在图1所说明的实施方案中，液体进料空气69被分成第一部分70和第二部分72。第一部分70，含有至少40％的液体进料空气69，并且可能含有高达100％的液体进料空气69，通过流经过冷器4被过冷然后如上所述作为流体71流入低压塔11。第二部分72，如果有的话，含有剩余的液体进料空气流69，流经阀73后作为液流74流入高压塔10。
于图1说明的本发明流入低压塔的液体进料空气在其引入低压塔之前被过冷的实施方案，在最大限度回收氧的方面是特别好的实施方案。
按常规的实施方法，如果进料空气被液化，则液化的进料空气要全部送入高压塔。由于在高压塔内发生的氩-氧分离甚微，所以进料空气中的大部分氩与来自高压塔的富氧底液一起流入低压塔。这样，与进入低压塔大流量的这种釜液(Kettle liquid)结合，使氩在釜液进料点下面的低压塔内得到浓缩，这样对从低压塔上部回收氩，以及回收氮都是有利的。
在流入低压塔的液化空气下实施本发明时，氩-氧分离出现在能使离开低压塔顶部的蒸气在保持低氧浓度的同时具有较高氩浓度的高压塔中。此外，液化空气对于低压塔能起中间回流液的作用，提高该塔那部分的液气比(L/V)，从而有助于分离。往低压塔引入液化空气还可以起到减小釜液从高压塔到低压塔的进料流速的作用，使氩在低压塔内向上移动。
当流体在高于塔温进入塔时，一些液体会被蒸发同时吸收由较高温度的流体所引入的热量。因此就指定流速而言，较热的进料向塔输送的液体回流液要比较冷进料少得多。过冷流入低压塔的进料空气凭借有效地向塔提供更多的回流液而有助于提高氧的回收。先过冷进料空气然后将其加入高压塔没有益处。在实施本发明时，低压塔在塔顶和液体空气加料点之间含有的平衡级比在常规低压塔中发现的多5-20。塔的这一部分完成挥发性更强组分的氮和氩与氧的分离任务。
在图1说明的本发明最佳实施方案中，采用第三进料空气部分。现再次参见图1，第三进料空气部分63，含有约4-10％的进料空气60，在压缩机30内进一步被压缩至范围在95-到160psia内的压力。所得到的进一步压缩进料空气第三部分64部分通过初级热交换器1被冷却再作为流体65通过流经涡轮膨胀机31涡轮膨胀。使所得到的涡轮膨胀过的第三进料空气部分66从涡轮膨胀机31流入低压塔11。正如图1所示，优选压缩机30与涡轮膨胀机31直接联用以便涡轮膨胀机31运转能起到驱动压缩机30的作用。
第一塔或高压塔通常在70-90psia范围内的压力下操作。在高压塔范围内，进料空气通过低温精馏被分离成为富氮蒸汽和富氧液体。富氮蒸汽作为流体79从高压塔10的上部排出再流入底部再沸器5，在那里富氮蒸汽通过与沸腾的低压塔11的底液间接热交换而被冷凝。所得到的富氮液体80被分成作为回流液流入高压塔上部的第一部分81，和通过流经过冷器2过冷的第二部分82。使过冷的富氮液流83流经阀84然后作为液流85流入低压塔11的上部成为回流液。富氧液体以液流75从高压塔的下部排出再通过流经过冷器3过冷。所得到的过冷富氧液流76流经阀77后作为液流78流入低压塔11。
第二塔或低压塔11在低于高压塔10的压力下且通常在18-25psia的范围内操作。在低压塔11内各种加到塔中的进料通过低温精馏被分离成液氧和废气。废气以气流89从低压塔11的顶部排出，通过流经过冷器2、3和4以及初级热交换器1废气升温再作为释放到大气的气流93从体系排放。
液氧作为流体86从低压塔11的下部排出。这是从低压塔11作为产品回收的唯一流体。如有要求，部分流体86还可作为液氧产品回收。在图1所说明的实施方案中，提高全部流体86的压力，如通过运用液体压头或如图1所说明的，通过运用液体泵33。高压液氧87通过流经初级热交换器1的产品锅炉部分借助与前述冷凝的进料空气第二部分间接热交换而被蒸发，然后作为具有至少98％(摩尔)氧浓度的高压氧气产品88且范围在40-250psia内的压力下进行回收。
图2说明本发明另外一种最佳实施方案，其中高压氮气被另外回收。对于通用的部件来说，图2中的数字与图1中的数字相当，并且这些通用的部件将不再作详细地描述。
现参照图2，第一进料空气部分61部分通过初级热交换器1。所得到的冷却进料空气流20通过流经涡轮膨胀机21而被涡轮膨胀，且所得到的涡轮膨胀进料空气第一部分22流入高压塔10。富氮蒸汽79的部分95通过流经初级热交换器1升温并作为具有至少99％(摩尔)氮浓度的高压氮气在范围为68-88psia的压力下回收。
现在通过本发明的使用人们能够使用双塔低温空气分离装置更加有效地生产高纯高压氧。尽管本发明参照某些最佳实施方案已详细予以描述，但所属领域的技术人员将会认识到在权利要求书的精神和范围内存在着本发明其它的实施方案。

Claims (10)

1．一种生产高压氧的方法，该方法包括：
(A)使进料空气的第一部分通入高压塔并且使来自该高压塔的流体通入低压塔；
(B)使进料空气的第二部分冷凝并使得到的液体进料空气通入低压塔；
(C)通过在低压塔内低温精馏生产液体氧；
(D)提高液体氧的压力以便生产高压液氧，并通过与冷凝的进料空气第二部分间接热交换使高压液氧蒸发以便生产高压氧气；和
(E)回收高压氧气。
2．权利要求1所述的方法，其中液体加料空气在进入低压塔之前被过冷。
3．权利要求1所述的方法，其中使部分液体进料空气进入高压塔。
4．权利要求1所述的方法，其中使进料空气的第一部分在进入高压塔之前涡轮膨胀。
5．权利要求1所述的方法，该法进一步包括涡轮膨胀进料空气的第三部分并使涡轮膨胀过的第三部分进入低压塔。
6．用于生产高压氧的设备，包括：
(A)第一塔、第二塔以及用于使进料空气进入第一塔的装置；
(B)产品锅炉、用于使进料空气进入产品锅炉的装置以及用于使来自产品锅炉的进料空气进入第二塔的装置；
(C)用于使来自第一塔的流体进入第二塔的装置；
(D)用于排出来自第二塔下部流体，提高排出的流体压力以及使排出的流体进入产品锅炉的装置；和
(E)用于从产品锅炉回收产品高压氧的装置。
7．权利要求6所述的设备，其中用于使来自产品锅炉的进料空气进入第二塔的装置包括过冷器。
8．权利要求6所述的设备，该设备还包括用于使来自产品锅炉的进料空气流入第一塔的装置。
9．权利要求6所述的设备，其中用于使进料空气进入第一塔的装置包括涡轮膨胀机。
10．权利要求6所述的制备，该设备还包括用于从第一塔的上部回收流体的装置。
CN98120912.2A 1997-10-14 1998-10-09 用于生产高压氧的低温精馏系统 Expired - Fee Related CN1123752C (zh)

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EP0909931A2 (en) 1999-04-21

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