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CN1210964A - 生产低纯氧的高压高效低温精馏系统 - Google Patents

生产低纯氧的高压高效低温精馏系统 Download PDF

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CN1210964A
CN1210964A CN98119107A CN98119107A CN1210964A CN 1210964 A CN1210964 A CN 1210964A CN 98119107 A CN98119107 A CN 98119107A CN 98119107 A CN98119107 A CN 98119107A CN 1210964 A CN1210964 A CN 1210964A
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pressure column
liquid
lower pressure
tower
nitrogen
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D·P·波纳奎斯特
S·M·萨坦
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Praxair Technology Inc
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Abstract

通过空气精馏生产低纯氧的高效系统使用高压塔和低压塔,和包括下列步骤:使来自高压塔的富氮气流进行涡轮膨胀,以提供冷却的富氮气流;与取自低压塔的蒸发富氧液流相逆流使冷却的富氮气流冷凝为富氮液体;将富氮液体作为回流液送往低压塔;使蒸发的氧液体返回到低压塔;利用涡轮膨胀步骤产生的能量来压缩原料空气。

Description

生产低纯氧的高压高效低温精馏系统
发明领域
本发明一般涉及低温空气分离，特别涉及生产低纯氧的低温空气分离。发明背景
与中等压力的氮共存的高压低纯氧有许多应用。煤气化和能源工业就是这些应用的实例。目前煤的气化消耗了大量的低纯氧。使用低纯氧发电也有很大的潜力。提供高压下的这些产物的经济来源是非常需要的。
目前提供与中等压力氮共存的高压低纯氧的工艺是采用常规的双塔循环，并且在低温分离后压缩产品气体。另一种方法是泵送液体产物，随后进行蒸发。在某些场合下，使用冷压缩来提供高压产物。这些可采用的方法的每一种都导致相当高的动力费用，以及相当高的投资费用。
据此，本发明的目的是提供具有高效率和低投资费用的生产低纯氧的低温空气分离系统。
本发明的另一个目的是提供改进的生产高压低纯氧的低温空气分离系统。
本发明的再一个目的是提供改进的生产高压低纯氧的低温空气分离系统，该分离系统也能生产高压氮。发明概述
本发明实现了上述目的和其它目的，通过阅读本文的公开，本领域的技术人员会很清楚这些目的的。本发明的一个方面是：
通过原料空气的精馏，生产低纯氧的低温精馏方法，所述方法采用了一高压塔和一低压塔，所述方法包括下述步骤：
(A)使从所述高压塔而来的富氮气流进行涡轮膨胀，以提供冷的富氮气流；
(B)与取自所述低压塔的蒸发富氧液流相逆流使所述冷的富氮气流冷凝为富氮液流；
(C)使所述的富氮液流作为回流液送回所述的低压塔；
(D)使所述的蒸发氧液流返回所述的低压塔；和
(E)利用所述的涡轮膨胀步骤(a)产生的能量。
本发明的另一个方面是：
生产低纯氧的低温精馏设备，包括：
(A)一高压塔，一低压塔，一压缩机和使原料空气从压缩机送到高压塔的装置；
(B)一涡轮膨胀机和使流体从高压塔的上部送到涡轮膨胀机的装置；
(C)热交换器，使流体从涡轮膨胀机送到热交换器和从热交换器送到低压塔的装置；
(D)使流体从低压塔送到热交换器和从热交换器送到低压塔的装置；和
(E)利用涡轮膨胀机产生的能量来运转压缩机的装置。附图的简要说明
图1是根据本发明第一个实施方案生产低纯气体氧系统的流程示意图。
图2是根据本发明第二个实施方案生产低纯气体氧的系统的流程示意图，该实施方案进一步可以生产液体氧。
图3是根据本发明第三个实施方案生产低纯氧的系统的流程示意图，该实施方案能生产液体氧，并能进一步生产低压气体氮。
图4是根据本发明第四个实施方案生产低纯氧的系统的流程示意图，该实施方案能生产液体氧，并能进一步生产低压气体氮。
图5是根据本发明第五个实施方案生产低纯氧的系统的流程示意图，该实施方案使用侧塔生产高纯液体氧。
附图的编号对于通用构件是相同的。
给本说明书和权利要求书中所使用的某些术语下定义一开始就是值得做的。
“塔”这一术语其含义是指蒸馏塔或分馏塔或者蒸馏区或分馏区，也就是说接触塔或接触区，液相和蒸汽相逆流流动，例如通过蒸汽相和液相在塔内固定的一系列垂直间隔的塔盘或塔板上和/或填料上的接触，以实现液体混合物的分离。为了进一步讨论蒸馏塔，请参看纽约.Mc Gyaw-Hill书籍出版公司的R.H.Perry和C.H.Chilton编辑的化学工程师手册第五版第13节B.D.Smith等人著的“蒸馏”篇，第13-3页题名为连续蒸馏法。使用“双塔”这一术语来表示一高压塔的上端与一低压塔下端有热交换的双塔。在1949年牛津大学出版社出版的第七章，工业空气分离中Ruheman著的“气体分离”一文有关于双塔的进一步讨论。
蒸汽和液体接触分离法取决于蒸汽压差。蒸馏是分离方法，藉此可以利用液体混合物的加热来浓缩蒸汽相中的挥发性组分和液相的难挥发组分。部分冷凝是分离方法，藉此可以利用蒸汽混合物的冷却来浓缩蒸汽相的挥发性组分，和因而可以浓缩液相的难挥发组分。精馏或称之为连续蒸馏也是分离的方法，该方法将蒸汽和液相的逆流处理所获得的逐级部分蒸发和冷凝结合起来。蒸汽相和液相的逆流接触是绝热的，它包括两相之间的积分接触和微分接触。利用精馏原理来分离混合物的分离法装置常常可互换地称为精馏塔、蒸馏塔或分馏塔。低温精馏至少部分地是在150°K或低于150°K的温度下进行的精馏法。
“低纯氧”的含意指的是含有小于或等于98％(摩尔)氧，优选地含有约90-98％(摩尔)氧的富氧液体。
本文所使用“涡轮膨胀”和“涡轮膨胀机”的术语其含意分别指的是高压气流通过涡轮而降低气体压力和温度从而产生致冷作用的方法和设备。
本文所使用“上部”和“下部”的术语其含意分别指的是塔中点以上和以下塔的部分。
本文所使用“间接热交换”的术语其含意指的是流体间没有任何物理接触或混合的两流体的热交换关系。
本文所使用当涉及塔时的“顶部”术语其含意指的是塔传质内部构件以上的部分，也就是塔盘或填料上方塔的部分。
本文所使用当涉及塔时的“底部”术语其含意指的是塔传质内部构件下方的部分，也就是塔盘或填料下方塔的部分。
本文所使用当涉及塔时的“中部”术语其含意指的是底部上方和顶部下方塔的部分。
本文所使用“原料空气”术语其含意指的是主要包含氧和氮的混合物，例如环境的空气。发明详述
简单地说，本发明采用热一体化的双塔空气蒸馏循环。双塔在高压下操作，高压塔一般在175-195psia之间进行操作，低压塔一般在60-70psia之间进行操作。用高压塔的氮来运转涡轮机，以低压塔液冷凝涡轮机流出物，优选地在中等水平，以提供致冷而使双塔热一体化。这种系统的动力需求约比常规的双塔系统小6％。由于涉及到较高的压力，该系统能够使用尺寸减小的工艺设备，这将导致投资费用的节省。
图1表示了体现本发明的双塔空气分离系统。利用压缩机10使原料空气125加压到约185psia，该原料空气已经清除了高沸点的杂质例如二氧化碳和水蒸汽。压缩机10的出料12约有一半作为物流16送往初级热交换器14，在其中冷却到接近饱和的温度。初级热交换器14的流出物流18送往高压塔20的底部作为该塔的初级进料。
压缩机10的出料约15％经管线22送往增压压缩机24，在其中加压到约222psia，然后送到初级热交换器14冷却到接近饱和的温度。然后作为物流26送到位于高压塔20底部的再沸器28。在这里原料空气用部分蒸发的底部富氧液体完全冷凝。这提供了高压塔20的上升蒸汽流。
再沸器28的冷凝液作为物流30送到氮过热器32，在其中冷凝液进行过冷，然后作为物流36送到低压塔34的中间部位。
送往此工厂的总空气约有33％经物流38送到高压压缩机40，在高压压缩机中压力加压到1300psia。输出物流42由此送往初级热交换器14，在初级热交换器中进行冷却(因为它首先加热，然后蒸发物流44中的逆流产物氧)。高压空气流46由初级热交换器14的冷端排出，在初级热交换器中冷端物流46通过阀门48节流到压力约185psia，然后作为物流50送往高压塔20。
富氧液流52从高压塔20的底部送往氮过热器32，在氮过热器中液流进行过冷，此后作为物流54送往低压塔34的中间部位。高压塔20顶部的富氮蒸汽作为物流56送往低压塔34中的主冷凝器58。在这里氮用部分沸腾产物液体氧冷凝为液体。所得到的液体氮60进行分流，一部分作为回流液126送往高压塔20的上部，另一部分作为回流液127送往低压塔34的上部。
来自高压塔20顶部的一部分富氮蒸汽流56作为物流62送往涡轮膨胀机64。如果需要的话，物流62在送往涡轮膨胀机64之前可以在初级热交换器14中进行加热。在涡轮膨胀机中产生了循环致冷。此外利用来自涡轮膨胀机64的动力输出来给例如在增压压缩机24中的输入空气加压。利用涡轮膨胀机与压缩机的间接或直接偶联，使涡轮膨胀机64的能量送往一台或多台原料空气压缩机，或者利用与涡轮膨胀机相连的发电机的发电使用发电机的电来运转一台或多台压缩机。这种操作导致了本发明实施中可大部分节能。
利用与来自低压塔34的部分蒸发富氧液流70的间接热交换，涡轮机64的排出物流66在热交换器68中完全冷凝。然后这种富氧物流作为物流72从热交换器68送到低压塔34。物流70优选地取自低压塔34的中间部位，和物料72也在中间部位送入低压塔34。来自热交换器68的液氮冷凝液作为物流74而被收集，此后送往氮过热器32。在过冷后，液氮冷凝液作为回流液76送入低压塔的上部，优选地送入顶部。如图1所示，物流74优选地与物流127合并而形成回流液76。
低压塔34优选在约62psia的压力下进行操作。低纯产物液氧作为物流78从低压塔底部抽出，和送入泵80，在泵80中它的压力增至所需要的高压，此处结合图1一道说明的特定例子中，所需要的高压约是1165psia。然后增压的低纯氧液体送往初级热交换器14的冷端，在热交换器中蒸发，加热到环境温度，再作为产物流82加以回收。
氮气作为物流84从低压塔顶部取出，送往氮过热器32，在过热器中，在送往初级热交换器14冷端之前，物流84被上述过冷物流加热。在初级热交换器14中，氮气加热到环境温度，并作为高压氮气流86供作最终使用。
上述的一体化循环获得超过98％的氧的回收率。计算表明该循环极大地降低了单位功率需求，一般约比带产品压缩机的常规双塔循环的单位功率需求低6％。由于比常规操作压力要高，本发明也因较小设备尺寸而降低了基本投资。
正如上述说明所能了解到的，使用高压塔氮经膨胀和被低压塔富氧液冷凝而产生致冷，就使低压塔和高压塔实现热一体化，从而降低了蒸馏系统的不可逆性。此外，高压塔在较高压力下运转不仅有助于这种特征的实现，而且也能够通过轴旋转做功而由涡轮膨胀机64回收能量。
当需要产生附加的液体时，在图2所示的高压物流42上可以安装两相涡轮膨胀机。这可以使约2.3％的氧作为液体除去。在这种情况下，图1例示的节流阀48被两相涡轮膨胀机100所代替。所需的高压空气数量的微小减少是由这种循环效率的改进。液氧产物流102是作为来自低压塔34底部的物流78的一支流而取出的。液体氧产物的主要部分连续地送往如前面图1所示的泵80。所有其它的特点仍旧相同。
图3表示了生产液氧的另一个可替代的方案。在这种情况下，利用过量氮膨胀机来提供平衡本方法(包括百分之几的液体)所需要的致冷。氮从初级热交换器14的中点提取出来用作涡轮膨胀机106的进料104。涡轮膨胀机106的排出物流108送往初级热交换器14的冷端，在此它作为低压气体氮输出之前被加热到环境温度。节流阀48代替图2的两相涡轮膨胀机100。图3的所有其它特征仍是相同的。
将图4所示的两相涡轮膨胀机100和过量氮涡轮膨胀机106相结合可以进一步增加液体的产量。根据这种安排，可以使液氧的产量增加到总氧产量的3.5％。这需要过量氮以入口空气2.3％的流速进行膨胀。
添加一个位于低压塔34下方的小侧塔110，如图5所示，可以产生高纯液氧。来自低压塔34底部的低纯液氧流112送到侧塔110的顶部。侧塔110顶部的蒸汽作为物流114回到低压塔34。侧塔110中纯净的下落液体富集了氧，并作为高纯(约99.5％)的氧流116在侧塔110底部取出。利用位于侧塔底部的再沸器118来运转侧塔110。高压塔20的蒸汽在再沸器118中冷凝，液体作为液流120返回到高压塔20。本法其余部分与图2所示使用两相涡轮膨胀机100的相同。
应该理解，上述的说明只是本发明例示性的说明。在不违背本发明的前提下，本领域的技术人员可以设计出不同的替代方案和改进方案。据此，本发明要包括所有这样的替代，改进和变化，它们都在所附权利要求的范围之内。

Claims (10)

1．以原料空气的精馏来生产低纯氧的低温精馏方法，该方法使用一高压塔和一低压塔，所述方法包括下列步骤：
(A)使来自所述高压塔的富氮气体流进行涡流膨胀以提供冷却的富氮气流；
(B)与取自所述低压塔的蒸发富氧液流相逆流使所述冷却的富氮气流冷凝为富氮液流；
(C)使所述的富氮液流作为回流液送回所述的低压塔；
(D)将所述的蒸发氧液流返回所述的低压塔；和
(E)利用所述的涡轮膨胀步骤(a)产生的能量。
2．权利要求1的方法，其中所述利用步骤是使用所述能量将原料空气流压缩至所述高压塔。
3．权利要求1的方法，还包括在所述涡轮膨胀之前通过与原料空气的间接热交换加热所述富氮气体。
4．权利要求1的方法，还包括在使作为回流液的所述富氮液体送往所述的低压塔之前，通过与来自所述低压塔的气体氮产物的间接热交换过冷所述富氮液体。
5．权利要求4的方法，还包括下列步骤：
使来自所述低压塔的所述气体氮产物流的一部分进行膨胀，以提供原料空气附加的致冷。
6．权利要求1的方法，其中使用初级热交换器来回收产物气体的致冷，所述方法还包括下列步骤：
通过所述的初级热交换器供给压缩空气，以提供冷却的压缩的原料空气；涡轮膨胀所述冷却的压缩的原料空气，以实现其进一步的冷却，然后将所述的冷却的压缩的原料空气送往所述高压塔；和
回收来自所述低压塔的富氧液体，和提供一部分富氧液体作为液体产物流出。
7．权利要求6的方法，还包括下列步骤：
涡轮膨胀一部分来自所述低压塔的气体氮产物流，以提供所述压缩原料空气的附加致冷。
8．权利要求1的方法，其中采用侧塔生产高纯氧，所述侧塔包括再沸器，所述方法还包括下列步骤：
将所述来自低压塔的低纯液体氧供给所述的侧塔；
将所述来自高压塔的蒸汽供给所述再沸器并使所述蒸汽与存在于所述侧塔中的液体氧逆流来冷凝所述的蒸汽，从而浓集所述的低纯氧；和
回收来自所述侧塔的高纯氧。
9．生产低纯氧的低温精馏设备，它包括：
(A)一高压塔，一低压塔，一压缩机和使原料空气从压缩机送往高压塔的装置；
(B)涡轮膨胀机和使液体从高压塔的上部送往涡轮膨胀机的装置；
(C)热交换器，将液体从涡轮膨胀机送往热交换器和从热交换器送往低压塔的装置；
(D)将液体从低压塔送往热交换器和从热交换器送往低压塔的装置；和
(E)利用涡轮膨胀机产生的能量来运转压缩机的装置。
10．权利要求9的设备，其中使液体从低压塔送往热交换器和从热交换器送往低压塔的装置在中间部位与低压塔连通。
CN98119107A 1997-09-09 1998-09-08 生产低纯氧的高压高效低温精馏系统 Pending CN1210964A (zh)

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CN103842753A (zh) * 2011-04-08 2014-06-04 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和设备
CN103842753B (zh) * 2011-04-08 2016-12-07 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和设备
CN112524886A (zh) * 2019-09-18 2021-03-19 乔治洛德方法研究和开发液化空气有限公司 高纯度氧生产系统

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