CN1045172A - 精馏分离空气的工艺及装置 - Google Patents

精馏分离空气的工艺及装置 Download PDF

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CN1045172A
CN1045172A CN90100334A CN90100334A CN1045172A CN 1045172 A CN1045172 A CN 1045172A CN 90100334 A CN90100334 A CN 90100334A CN 90100334 A CN90100334 A CN 90100334A CN 1045172 A CN1045172 A CN 1045172A
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medium pressure
argon
oxygen
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CN1025067C (zh
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迪特里希·罗特曼
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Linde GmbH
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Abstract

本发明披露了藉精馏并接着制取粗氩的空气分离工艺及装置。粗氩精馏段20的运行压力比两级空气精馏段2的中压级4的压力要低。

Description

本发明主题是精馏分离空气的工艺，其中将空气压缩、预净化、冷却，然后在两级精馏段的增压级中，预分离成富氮馏份和富氧液体，并将这两种馏份至少部分地输入精馏段的中压级，然后分离成氧和氮，而且其中将含氩的氧流从中压级抽出并送往粗氩精馏段;本发明的主题还是实施该工艺的装置。
这样一种工艺，其中分离空气后紧接着制取粗氩，已由联邦德国专利局公开说明书DE-OS    3436897所公知。
如同在迄今运用的工艺中所习以为常的那样，在先前已公开的工艺中，粗氩的精馏是在含氩的氧馏份由中压级取出的压力条件下进行的。液态氧从粗氩精馏段输至中压级大体相同的部位。
如果中压级基本上在大气压力下工作，从而粗氩精馏也基本上在大气压力下进行，则这样一种工艺是有利的。在许多情况下，在中压级产生的氧和/或氮却需处于高压下，例如在煤炭气化装置中或者为在采油采气时进行吹氮。因此，为获得压缩的氮和氧，经济上有利的做法是，使中压级在约2.0～8.0bar的高压下运行，接着作为无压力情况下获得的产物予以压缩。
但由于在已知方法中，粗氩精馏段必须在高压下运行，故而也产生一些不足之处，因为在此前提下，只能达到相当小的氩产率。
本发明所基于的任务是：将本说明书起首所述的那种工艺及装置加以改进，使之不仅能经济地生产压缩氮和压缩氧，而且也能以低成本制取氩。
此项任务是通过使粗氩精馏段在低于中压级压力的条件下运行，来解决的。
因此，粗氩精馏时的压力比不再受中压级压力比约束，从而可保持对氩产率来说最佳的值为1.1～2.0bar，优选1.3～1.5bar。尽管如此，中压级还能在高压下放出氧和氮。
本发明的工艺，在含氩的氧流被输入粗氩精馏段之前，先予以作功减压时，被证明有其优越之处。减压时所回收的能量，可用来压缩其它工艺料流。除此以外，作功减压时产生特别多的、分离空气所需的冷量。以此方法，至少可以部分地取消外加制冷的输入。
因而，有利的做法是在作功减压之前，将含氩的氧流加热。这可通过与其它的工艺料流换热来进行，以与待分离的空气换热来进行为佳。
通常以液态产生的粗氩精馏残余馏份，主要由氧组成。由于将此馏份废弃是不经济的，所以本发明的另一特征建议，将该液态馏份从粗氩精馏段回输至中压级，并在输入中压级之前，用泵增至中压级的压力。
事实证明，当使粗氩精馏塔顶的气相馏份通过与来自增压级的、蒸发着的富氧液体进行间接换热而冷凝时，这是有利的。以此方法，可利用工艺中现有的冷量来形成供粗氩精馏用的回流，并可取消在此工作区使用外加冷量。
由此产生的被蒸发富氧馏份，以回输到中压级为佳。
被蒸发的富氧馏份，须在输入中压级之前予以压缩。为此目的，按本发明工艺的另一种方案，将含氩的氧流作功减压时所得到的功，至少部分地用来压缩被蒸发的富氧馏份。
此外，将被蒸发的富氧馏份压缩后进行冷却，这也是有利的。
本发明还涉及一种实施本发明所述的精馏分离空气的工艺的装置。
附图中用示意图示出了本发明工艺的一种实施方式，下面根据该图来进一步阐述本发明及本发明的其它细节。
经压缩并预净化的空气，经由管道1引入，在换热器36中经与产物流间接换热而冷却，并输入两级精馏塔2的增压级3。增压级3（工作压力：6～20bar，以8～17bar为佳）同中压级4（工作压力：1.5～10bar，以2.0～8.0bar为佳）经共用的冷凝器/蒸发器13发生换热联系。输入的空气在增压级3中预分离成氮和富氧馏份。该富氧馏份经由管道6冷却成液态，在换热器32中过冷，并有一部分经由管道10减压输入中压级4。由增压级3顶部出来的氮经由管道5同样以液态抽出，在换热器32中过冷，并有一部分经由管道8作为液态产物排出。由增压级3出来的另一部分氮，经由管道9作为回流送到中压级4。
液态氧（管道14）、气态纯氮（管道15）及不纯氮（管道16）作为中压级4的产物予以抽出，并在换热器36中加热，氮流还外加在换热器32中加热。
除了至此已提及的物流外，还有一种含氩的氧流经由管道17从中压级4抽出，在换热器36中加热，并输入粗氩精馏段20，该段在1.1～2.0bar的压力下工作，以在1.3～1.5bar的压力下工作为佳。在粗氩精馏段20底部产生的残余馏份经由管道22予以抽出，并按本发明用泵23增压到向中压级4回输所需的压力。除此以外，还使富氩氧流17在输入粗氩精馏段20之前，在减压涡轮机18中作功减压，使之一方面减到粗氩精馏段所存在的低压，另一方面产生工艺冷量。
在粗氩精馏段20顶部产生的气态粗氩，经由管道33导入冷凝器35，部分液化，并有一部分经由管道34作为回流输回粗氩精馏段20，另一部分经由管道21作为中间产物抽出，并在换热器36中予以加热。
冷凝器35由来自增压级的一部分富氧馏份6冷却，该馏份经由管道11引来，在换热器24中过冷，并经由管道25导入冷凝器35。在同粗氩精馏段20的塔顶气体进行间接换热时被蒸发的那部分，经由管道26抽出，并在换热器24及36中予以加热。
由于将该物流中所含的氧废弃，在经济上不合算，所以在实施例的工艺中，将其回输到中压级4。为达到为此所需的压力，将该富氧物流在两个压缩级27及29中进行压缩，并各随后进行冷却（水冷却器28及30）。接着，将富氧物流经由管道32输经换热器36，在此再予冷却，并随后输至中压级4。此时，有利的是将在含氩的氧馏份17减压时所得的功用来驱动压缩机29。
在输入增压级3之前，可将管道1中的一部分空气，在换热器中用来自中压级4底部的氧予以冷凝。为此，可将来自中压级底部的液体用泵增至高压，并在换热时部分蒸发。然后将部分冷凝的空气在高于附图所示的第一输入部位（管道1）的位置输入增压级3。该工艺部位在附图中未示出，但在给定的精馏压力下可以是有利的。
对于有经济意义的氩产率来说，必须生产出纯度至少为99.5%的产品氧（管道14），以便在富氩的氧流（管道17）中富集足量的氩。为此，在中压级4中压力为5bar时，常规工艺需要的空气系数为5.86。而在本发明工艺中该系数则减至5.45。从而节省能量7.0%。

Claims (13)

1、精馏分离空气的工艺，其中空气1经压缩、预净化、冷却36，以及在两级精馏段2的增压级3中预分离成富氮馏份5和富氧液体6，并将这两种馏份5、6至少部分地输入精馏段2的中压级4，然后分离成氧和氮，而且在其中，将含氩的氧流17从中压级4抽出，并输向粗氩精馏段20，其特征在于，粗氩精馏段20的运行压力低于中压级4的工作压力。
2、权利要求1所述的工艺，其特征在于，含氩的氧流17在被引入粗氩精馏段20之前先作功减压。
3、权利要求2所述的工艺，其特征在于，含氩的氧流17在作功减压18之前先进行加热。
4、权利要求1至3中任一项所述的工艺，其特征在于，将来自粗氩精馏段20的液态馏份20回输至中压级4，并在输入中压级4之前用泵23增至中压级4的压力。
5、权利要求1至4中任一项所述的工艺，其特征在于，使粗氩精馏段20顶部的气态馏份33在间接换热35过程中，用来自增压级3的蒸发着的富氧液体25进行冷凝。
6、权利要求5所述的工艺，其特征在于，将蒸发过的富氧馏份26回输到中压级4。
7、权利要求6所述的工艺，其特征在于，将蒸发过的富氧馏份26在输入中压级4之前进行压缩27、29。
8、权利要求2及7所述的工艺，其特征在于，至少部分地将含氩的氧流17作功减压18时所得的功，用来压缩29已蒸发的富氧馏份26。
9、权利要求7或8所述的工艺，其特征在于，使已蒸发的富氧馏份31在压缩27、29后进行冷却36。
10、实施权利要求1至9任一项所述工艺用的装置，该装置包括一座由增压级3和中压级4构成的双层精馏塔2，并包括一座粗氩精馏塔20和位于中压塔4和粗氩精馏塔20之间的第一连接管道17、19及第二连接管道22，其特征在于，在第一连接管道17、19中，装有减压装置18。
11、权利要求10所述的装置，其特征在于，在第二连接管道22中装有一台泵23。
12、权利要求10或11所述的装置，其特征在于，包括一台经由第一气体导管33及经由第一液体导管34与粗氩精馏塔20连通，并经由第二液体导管25与增压塔3连通的换热器35，一根使换热器35与中压塔4连通的第二气体导管26、31，以及一台位于第二气体导管26、31上的压缩机27、29。
13、权利要求12所述的装置，其特征在于，将一台膨胀式涡轮机用作减压装置18，并使该机同第二气体导管上的压缩机29偶联。
CN90100334A 1989-02-23 1990-01-23 精馏分离空气的方法及装置 Expired - Fee Related CN1025067C (zh)

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CN1025067C (zh) 1994-06-15
US5034043A (en) 1991-07-23
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