CN1116293A - 生产高压氧气的空气沸腾低温精馏系统 - Google Patents

生产高压氧气的空气沸腾低温精馏系统 Download PDF

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CN1116293A
CN1116293A CN95105471A CN95105471A CN1116293A CN 1116293 A CN1116293 A CN 1116293A CN 95105471 A CN95105471 A CN 95105471A CN 95105471 A CN95105471 A CN 95105471A CN 1116293 A CN1116293 A CN 1116293A
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G·A·包林诺
R·F·德尼维希
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Praxair Technology Inc
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Abstract

一种空气沸腾低温精馏系统，其中附加的进料空气气流被用来使加压的液态氧汽化，并通过涡轮膨胀，在进入塔系统之前使其冷却。

Description

生产高压氧气的空气沸腾低温 精馏系统
本发明通常涉及采用空气沸腾的低温精馏工艺，它尤其有助于生产氧气浓度在70～85摩尔百分数范围内的高压氧气。
低温精馏空气的生产氧气和氮气是一个早已制定的工业方法。通常在双塔系统中对进料空气进行分离，其中来自高压塔的氮气或顶部蒸汽被用来使低压塔中的底部液态氧再沸腾。
对低纯度氧气的需求在不断增加，例如在玻璃制造业、炼钢和能源生产中都要使用低纯度氧气，对于生产低纯度(氧气纯度小于98.5摩尔百分数)的氧气来说，必须使在低压塔的汽提段蒸出的蒸汽和在低压塔的富集段回流的液体，少于通常双塔运行所产生的蒸出蒸汽和回流液体。
因此，采用一个低温精馏系统可以生产大量的低纯度氧气，其中进料空气在高压塔的压力下，被用于使低压塔底部的液体再沸腾，然后，再进入高压塔。要使用空气而不是氮气来使低压塔底部液体汽化，这样作可以降低对进料空气压力的要求，并且，或者通过在低压塔的再沸器中输入适量的空气，或者通过使总进料空气的较大部分被部分冷凝，以使在低压塔的汽提段只作必要的沸腾。
尽管传统的空气沸腾低温精馏系统能够有效地生产低纯度氧气，但它在产生液态氮回流液以供应到低压塔顶部方面的能力却受到限制。这起因于在高压塔的运行压力下，组分较低的相对挥发性，该高压塔类似于主空气进料塔，这是由于产生了大量的液态空气。此外，由于产生液态氮回流液的能力也降低，使得回收的氧量减少，从而增加了能量消耗。
因此，本发明的一个目的是提供一种生产低纯度氧气的低温精馏系统，其中通过与进料空气进行间接热交换，使低压塔底部的液体再次沸腾。与传统的空气沸腾系统的能量需求相比，尤其是在生产的氧气浓度小于90摩尔数的情况下，本发明的系统可在降低能量需求的条件下运行。
经常希望在高压下回收氧气产品，通常可以通过使气体穿过一个压缩机，而将产品气体压缩到高压力。这种系统有效，但成本高。此外，至今空气沸腾低温精馏系统已被大量地用于生产低压氧气。
因此，本发明的另一个目的是提供一种空气沸腾低温精馏系统，该系统能够在无需对氧气进行压缩的情况下，高效率生产高压氧气。
本专业技术人员在阅读了本发明的说明书后就会清楚本发明的上述目的和其它目的，通过实施本发明可以实现这些目的，本发明的一方面是：
一种采用高压塔和低压塔的低温空气分离方法，其中采用进料空气使低压塔底部的液体沸腾，然后将进料空气通入高压塔中，并在低压塔中产生液态氧，本发明的改进之处包括：
(A)对第二部分进料空气进行涡轮膨胀，以产生冷却，将涡轮膨胀后的第二部分进料空气通入高压塔中；
(B)从低压塔排出液态氧，并增加所排出的液态氧的压力；
(C)通过与第三部分进料空气进行间接热交换，使加压后液态氧汽化，第三部分进料空气的压力高于使低压塔底部液体沸腾的那部分进料空气的压力，从而生成了氧气和液态进料空气；
(D)将生成的液态进料空气通入至少高压塔和低压塔中的一个塔；以及
(E)回收生成的氧气作为高压氧气产品。
本发明的另一方面是：
一种低温精馏装置，有第一塔和底部带有再沸器的第二塔，以及将进料气流输送到底部再沸器，并从底部再沸器输送到第一塔中的部件，改进之处包括：
(A)一个涡轮膨胀机，和将第二部分进料气流输送到涡轮膨胀机以及从涡轮膨胀机输送到第一塔中的部件；
(B)从第二塔中排出液体的部件，以及用于对从第二塔排出的液体加压，以生产高压液体的部件；
(C)一个产品沸腾器，将第三部分进料气流输送到产品沸腾器中的部件，以及将上述高压液体输送到产品沸腾器中的部件；
(D)将液态进料空气从产品沸腾器输送到第一塔和第二塔中的至少一个塔中的部件；以及
(E)从产品沸腾器回收气体产品的部件。
这里所使用的“液态氧”这一术语表示氧的浓度的70～98摩尔百分数范围内的液体。
这里所使用的“进料空气”这一术语表示最初含有氮气和氧气的混合物，如空气。
这里所使用的术语“涡轮膨胀”和“涡轮膨胀机”分别代表一种方法和一种装置，该方法和装置是使高压气体流过一个涡轮机，以降低气体的压力和温度，从而使其冷却。
这里所使用的“塔”这一术语表示分馏蒸馏塔或区，即：一个接触塔或区，其中液相和蒸汽相逆流接触，以有效地分离流体混合物，例如，通过使蒸汽相和液相在安装在塔中一组垂直隔开的塔盘或塔板上的接触，和/或在填充元件上的接触，上述填充元件可以是规则填充和/或不规则填充元件。对蒸馏塔进一步的论述见由R.H.Perry和C.H.Chilton，McGraw-Hill BookCompany，New York出版的《化学工程师手册》第五版，第13章“连续蒸馏工艺”。
蒸汽和液体的接触分离过程，取决于组分的蒸汽压的差别。蒸汽压高(或挥发性高或沸点低)的组分趋于在汽相浓缩，而蒸汽压低(或挥发性低或沸点高)的组分则趋于在液相浓缩。部分冷凝就是冷却蒸汽混合物可以用来浓缩汽相中的挥发性组分(多个挥发组分)，从而使低挥发性组分(多个挥发组分)在液相中浓缩的分离过程。精馏或连续蒸馏也是一种通过使汽相和液相逆流处理而得到的连续部分汽化和冷凝结合起来的分离方法。汽相和液相的逆流接触是不传热的，两相之间可以是积分接触或微分接触。利用精馏原理分离混合物的分离过程设备，在称呼上经常是可互换的，如精馏塔、蒸馏塔或分馏塔。低温精馏是一种精馏方法，该方法至少部分在150°或低于此温度下进行。
这里所使用的“间接热交换”这一术语表示在没有任何物质接触或流体之间相互混合的情况下，使两种流体物料进行热交换。
这里所使用的术语“顶部冷凝器”表示一种使塔顶蒸汽生成向下流动的液体的热交换设备。
这里所使用的术语“底部再沸器”表示一种使塔底液体生成向上流动的蒸汽的热交换设备。
图1是本发明一个最佳实施例的简图。
图2是本发明另一最佳实施例的简图。
下面参照附图对本发明进行详细描述。
参照图1，通常在40～65磅/英寸2的绝对压力(Psia)的进料空气1，通过在热交换器300中与回流物流进行间接热交换而被冷却，结果生成了进料空气气流2，它通过穿过热交换器301而被进一步冷却。得到的进料空气气流3，流入底部再沸器306，在这里它被部分冷凝，同时使低压塔200底部的液体沸腾，低压塔200通常在18～25psia的压力范围内运行。得到的进料空气以气流4的形式，从再沸器306的底部进入高压塔100，该高压塔100在高于低压塔200的压力下运行，压力范围通常为30～60psia。
另一输入的空气气流10，在大于气流1的压力下，通常在80～1400psia的压力范围内，由穿过热交换器300而被冷却。得到的进料空气气流11被分成气流25和气流12。气流25包括第二部分的进料空气，它由穿过涡轮膨胀器35被涡轮膨胀而产生制冷作用。得到的进料空气气流26由穿过热交换器309而被降温，再以气流27进入高压塔100。
气流12由穿过热交换器301而被进一步冷却，至接近其饱和点，得到的进料空气气流14被分成气流5和气流15。气流15由穿过热交换器305而液化，得到的液化进料空气6进入塔中，下面还将进行详细描述。
气流15包括第三部分的进料空气，其压力高于沸腾低压塔200底部的进料空气的压力。气流15进入产品沸腾器307，在这里它通过与汽化的加压液态氧间接进行热交换而被冷凝，然后进入塔100和塔200中的至少一个中。图1所表示的实施例是一个最佳实施例，其中生成的液态进料空气沿管线16进入低温冷却308中，在这里通过与加压液态氧进行间接热交换而被低温冷却。低温冷却后的液态进料空气17，与液流6结合在一起，形成进料空气液流18，该液流18由穿过热交换器304而被进一步低温冷却，形成液流19。
液态进料空气19的至少一部分22穿过阀40，其压力被调节到高压塔100的压力，由此得到的进料气流23进入高压塔100内。如果需要，可使液态进料空气19的一部分20穿过阀50，将其压力调节到低压塔200的压力，得到的进料空气部分21进入低压塔200中。
在高压塔100内，通过低温精馏将进料空气分离成富氮蒸气和富氧液体。富氮蒸气70进入顶部的冷凝器302，在那里被冷凝。生成的液体分成回流液46和73。回流液73作为回流进入高压塔100中。回流液46穿过热交换器303而被低温冷却，得到的液流47穿过阀门48将其压力调节到低压塔200的压力，并作为回流液49进入低压塔200中。如果需要，富氮蒸汽的一部分42可由通过热交换器301和300而被加热，并作为高压氮气产品而被回收，其纯度高达大约99.9摩尔百分数。
富氧液体的液流28的形式穿过热交换器304，在其中被过冷。得到的液流29穿过阀门37而被减压，得到的液流30进入冷凝器302，在这里通过与冷凝的富氮蒸汽进行间接的热交换而被部分汽化。得到的富氧蒸汽和剩余的富氧液分别以气流32和液流31的形式，分别穿过阀门38和39，并在其中将其压力减压到低压塔200的压力。然后，分别得到的气流34和液流33进入低压塔200内。
通过在塔200内进行低温精馏使进入低压塔200中的各种物料分离，产生氮蒸汽和液态氧。氮蒸汽以气流51的形式从塔200中排出，穿过热交换器303、304、305、301和300而被加热，如果需要，可作为低压氮气产品55回收，其氮气的纯度高达大约99.5摩尔百分数。
以液流58的形式从低压塔200中排出的液态氮，例如通过穿过一个液体泵59而被加压。然后，得到的加压液氧60在热交换器308中由对液态进料空气低温冷却而被加热，再以液流61的形式进入产品沸腾器307中，在这里通过与加压的进料空气进行间接的热交换而被汽化。在产品沸腾器中产生的氧气以气流62的形式穿过热交换器309、301和300，在这些热交换器中，它被加热，作为高压氧气产品被回收。通常其压力在40～800psia范围内，氧气浓度在70～98摩尔百分数范围内。
图2表示的是本发明的另一实施例，对一般的部件，图2中数字表示的部件与图1中的部件相同，在此不再详细地描述。图2所表示的实施例与图1所表示的实施例的不同之处首先在于，经涡轮膨胀后的进料空气26在穿过热交换器309后，不是直接进入高压塔100，而是与气流3结合在一起，形成进料空气气流91，该气流91在进入底部再沸腾306之前，先穿过热交换器301，然后以气流4的形式进入高压塔100中。在图2所示实施例的实际运行中，高压进料空气气流14，以及氧气气流62和氮气气流42和51都穿过热交换器310。
本发明优于传统的空气沸腾系统之处在于，在氧气纯度小于90摩尔百分数，尤其是在70～85摩尔百分数的范围内，本发明能够高效率地生产氧气。采用传统工艺，当氧气纯度小于90摩尔百分数时，会出现这种情况，涡轮机前后的压力比太小，以致于不能产生足够的致冷的维护工艺的运行。由于本发明使高压进料空气气流流入涡轮机内，所以本发明解决了这个难题。
尽管参照特定的最佳实施例对本发明进行了详细地描述，但本专业技术人员应该知道，在本发明的精神和权利要求书的范围内，本发明还会有其他的实施方案。

Claims (7)

1.一种采用一个高压塔和一个低压塔的低温空气分离方法，其中使用进料空气使低压塔底部的液体沸腾，然后再将其通入高压塔中，并在低压塔中生成了液态氧，本发明的改进包括：
(A)使第二部分进料空气涡轮膨胀，以使其冷却，并将涡轮膨胀后的第二部分进料空气通入高压塔中；
(B)从低压塔排出液态氧，并增大所排出的液态氧的压力；
(C)通过与第三部分进料空气进行间接热交换，使加压后的液态氧汽化，第三部分进料空气的压力高于那部分使低压塔底部的液体沸腾的进料空气的压力，从而产生了氧气和液态进料空气；
(D)将生成的液态进料空气通入高压塔和低压塔中的至少一个塔；以及
(E)回收生成的氧气作为高压氧气产品。
2.如权利要求1所述的方法，其特征在于在进入高压塔之前采用涡轮膨胀后的第二部分进料空气使低压塔底的液体沸腾。
3.如权利要求1所述的方法，其特征在于将生成的液态进料空气既通入高压塔，又通入低压塔。
4.如权利要求1所述的方法，其特征还在于包括在高压塔和低压塔中的每一个塔中都产生氮气蒸汽，从高压塔和低压塔中至少一个塔中回收氮气蒸汽，作为氮气产品。
5.一种低温精馏装置，包括第一塔和带有底部再沸器的第二塔，将进料气流输送到底部再沸器并从底部再沸器输送到第一塔的部件，改进之处包括：
(A)一个涡轮膨胀机，和将第二部分进料气流输送到涡轮膨胀机以及从涡轮膨胀机输送到第一塔中的部件；
(B)从第二塔中排出液体的部件，以及用于给从第二塔排出的液体加压，以生产高压液体的部件；
(C)一个产品沸腾器，将第三部分进料气流输送到产品沸腾器中的部件，以及将上述高压液体输送到产品沸腾器中的部件；
(D)将液态进料空气从产品沸腾器输送到第一塔和第二塔中的至少一个塔中的部件，以及
(E)从产品沸腾器回收气体产品的部件。
6.如权利要求5所述的装置，其特征在于将第二部分进料气流从涡轮膨胀机输送到第一塔的部件包括一个底部再沸器。
7.如权利要求5所述的装置，包括将液态进料从产品沸腾器既输送到第一塔又输送到第二塔中的部件。
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