CN1025068C - 通过精馏来分离空气的方法和装置 - Google Patents

通过精馏来分离空气的方法和装置 Download PDF

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CN1025068C
CN1025068C CN90100335A CN90100335A CN1025068C CN 1025068 C CN1025068 C CN 1025068C CN 90100335 A CN90100335 A CN 90100335A CN 90100335 A CN90100335 A CN 90100335A CN 1025068 C CN1025068 C CN 1025068C
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pipeline
nitrogen
heat exchanger
cut
pressure
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CN1045173A (zh
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迪特里希·罗特曼
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Linde GmbH
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Linde GmbH
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Abstract

本发明描述了通过精馏来分离空气的一种方法和一种装置。将由工艺流程中抽出的氮经管道(16)抽出并加热到一中等温度，从主换热器(17)中抽出一部分经管道(30)导出，再经透平膨胀机31作功膨胀。经膨胀的气体由管道(43)送入主换热器(17)中将其冷量传给待分离空气(由管道送入)，然后重新压缩(经压缩机33、36)此部分膨胀过的气体。

Description

本发明涉及一种通过精馏来分离空气的方法，其中对空气进行压缩、预净化、冷却并在两级精馏的高压级中粗分馏成富氮馏分和富氧液体，将这两种馏分至少部分地送往精馏的中压级，分离成氧和氮，同时，至少抽出气态氮馏分，加热并使其至少部分地作功膨胀。另外，本发明还涉及实施该方法的装置。
美国专利说明书US2，666，303公开了一种这样的方法。其中，使来自中压级的氮减压膨胀以便得到工艺流程所需的冷量。这比中压级在高于大气压力下运行时用高压级氮作为制冷循环的工质要经济。然而，该已知方法的缺点是，中压级气态氮馏分已减压的部分不能再用于需要高压的用途。
本发明的目的在于提高本说明书开头所述类型的方法和装置的经济性，尤其是要以特别有利的方式提供工艺流程所需的冷量，且不限制气态氮馏分的继续应用。
该目的可由下述措施来实现：加热并重新压缩至少一部分作功膨胀后的氮，同时将至少一部分减压膨胀所得的功用于压缩。
由于透平膨胀机入口处的压力还相当高，因而可以达到较高的效率，所以在高压下运行的空气分离装置中进行作功膨胀和再压缩，这对于与发电装置联合且都是用煤或重油的气化来驱动的空气分离装置来说，尤为适宜。
从流程之外输入能量作为压缩功的一部分，这证明是有利的。如果要求再使用的氮气的参数与原来的参数一致的话，用此措施可使减压后的氮气部分重新恢复其原有的压力（减压前的压力）或上升到更高的压力。例如，在空气分离设备与煤气化发电装置的联合设备中，可将再压缩的氮气送入通常处于高压下的燃烧室。
按本发明另一特征使气态氮馏分减压的部分压缩到基本上与气态氮馏分分开时相等的压力，接着再将其送入气态氮馏分未减压的部分中尤为有利。
借助于这种工艺过程，按照本发明制冷时，还可以将处于中压级（一般压力较高）压力下的全部气态氮馏分，例如提供给一个煤气化发电装置的燃 烧室继续使用。
尤其在整个空气分离和特别是中压级必须在较高压力下运行的那些应用中，所达到的产品纯度往往是不能令人满意的。得到的氮气纯度不高，氧气产品则纯度更差。
由于这种原因，按照本发明的另一方面，从中压级顶部抽出另一部分氮馏分，将之加热，压缩，接着再冷却并导入高压级，在一定的情况下是有益的。将（纯）氮馏分至少部分地送入一个所谓的强化循环中。经由强化循环而进入高压级的氮与中压级的釜液间接换热而被冷凝，再以液态形式被抽出并作为附加回流液供给中压级。由此，在不影响高压级传质的条件下提高了中压级的物质交换，因而产品流具有较高的纯度。
本发明还涉及一种实施上述方法的装置。该装置包括一个主换热器，该换热器内有空气和氮气通道，还具有一个由高压塔和中压塔组成的双级精馏塔，其特征是有一根管道由主换热器的中间区域引出，使氮气通道与透平膨胀机入口连通，并用另一根管道将透平膨胀机出口与一台压缩机的入口连通，并作为通道穿过主换热器。此外，压缩机的出口还可以与主换热器的氮通道的出口连通。
下面借助于附图所示本发明方法的一种实施方式进一步解释本发明及其它细节。
经压缩及预净化的空气经管道1导入，在主换热器17中与产品流间接换热而冷却，然后进入两级精馏塔2的高压塔3。用一个公用的冷凝器/蒸发器13使高压塔3（操作压力：6至20巴，优选8至17巴）与中压塔4（操作压力：1.5至10巴，优选2.0至8.0巴）相连，并使二者进行热交换。引入的空气在高压塔3中被粗分离成氮和富氧馏分。富氧馏分经管道6以液体状态抽出，在换热器32中过冷后节流喷入中压塔4。高压塔3顶部的氮同样以液体形式经管道5抽出，在换热器32中过冷后其中一部分由管道8作为液态产品抽出。来自高压塔3的另一部分氮由管道9作为回流送入中压塔4。
液体氧（经管道14）、气态纯氮（经管道15）和不纯的氮（经管道16）作为中压塔4的产品提取，并在主换热器17中被加热，上述两股氮气流则另外还在换热器32中辅助加热。
使管道1中一部分空气（经管道21）在进入高压塔3之前在换热器20中与来自中压塔4塔釜的氧（经管道14）换热而冷凝。为此来自中压塔4塔釜的液氧（经管道14）由泵19加压到高压，并在冷凝器20中进行热交换时部分地汽化。部分已冷凝的空气经管道22在高于第一进料口（经管道1）的位置进入高压塔3。氧的汽化部分由管道23排出并被加热（经换热器17）。另一部分氧由管道42作为液体产品流抽出。
按照本发明，使管道16中的一部分不纯的氮在约110至210K、优选135至185K的中等温度下经管道30从主换热器17中引出，并在透平膨胀机31中作功膨胀到2.6至1.4巴、最好膨胀到约2.0巴的压力。减压膨胀后的氮经管道43重新送到主换热器17的冷端并加热到大致为环境温度。从而将减压膨胀时获得的冷量传递给管道1中待分离的空气。
为了能够使膨胀的氮和未膨胀的部分（流经管道39的部分）一起抽出，应将已膨胀的氮再经两级33、36压缩，并将各级压缩热带走（由冷却器35、37带走）。第二压缩级36与透平膨胀机31相耦合，以便回收膨胀时所作的功用于工艺流程中。为了使该气体重新恢复其（在管30及29中的压力）初始压力，还需要另一压缩级33，该压缩级由外部引入的能量驱动。然而，通过本发明的方法，此部分附加消耗的能量能非常有效地转化成工艺流程所需的冷量。
如果需要压力高于中压塔4的压力的纯氮，可在加热后将其压缩。这一般在多个压缩级40、41中实现。此时，通常在每级40、41之后，要用水冷却器（图中未示出）将压缩热导出。
在这种情况下，特别有利的是采用强化循环来提高中压塔的传质和产品纯度。为此，图中虚线表示的管线是必要的。至少将来自管道15的一部分纯氮调整到高压塔（在该实施例中位于压缩级40和41之间）的压力，经管道42抽出，并在主换热器17中加热，继而经管道42送入高压塔3。
所补充的氮在中压塔4的顶部冷凝，同时液体在其塔釜汽化。它还可以液体形式附带经管5采出，并以回流形式送入中压塔。然后也由管15采出数量相应提高的氮，将之加热（32，17）并在压缩级40压缩，这样，强化循环通路就闭合了，实现了换热器32和17的平衡。

Claims (7)

1、通过精馏来分离空气的方法，其中将空气(经管道1)压缩、预净化、冷却(经主换热器17)并在两级精馏塔(2)的高压级(3)粗分离成富氮馏分(经管道5)和富氧液体(经管道6)，该两种馏分至少部分地进入精馏塔(2)的中压级(4)，并分离成氧和氮，其中至少引出一种气态的氮馏分(经管道16)，使其加热(经主换热器17)并至少部分地(由管道30抽出)作功膨胀(经膨胀机31)，其特征在于，将至少一部分作功膨胀(经膨胀机31)过的氮(经管道43)，加热(经主换热器17)并重新压缩(经压缩级33，36)，其中将膨胀(经膨胀机31)时所得功的至少一部分用于压缩。
2、如权利要求1所述的方法，其特征是，压缩级（33）的一部分功率由工艺流程之外输入的能量供给。
3、如权利要求1或2所述的方法，其特征是，将气态氮馏分膨胀后的部分（经管道43）压缩（由压缩级33、36压缩）到与气态氮馏分（管道16中的馏分）的分支（管道30、39中的馏分）的压力基本相等的压力。
4、如权利要求3所述的方法，其特征是，将气态氮馏分膨胀并重新压缩的部分（经管道38）重新引入气态氮馏分未减压膨胀的部分（管道39中的馏分）。
5、如权利要求1至4中任一项所述的方法，其特征是，由中压级（4）顶部抽出另一股氮馏分（经管道15），将之加热（经换热器32、17），压缩（经压缩机40），接着再次冷却（经换热器17）并经管道（42）引入高压级（3）。
6、实施权利要求1至5中任一项所述方法的装置，该装置中有一个主换热器17，其内有空气通道（1）和氮通道（16、39），有一个由高压塔（3）和中压塔（4）组成的双级精馏塔（2），其特征在于，管道（30）由主换热器（17）的中间区域引出并与氮通道（16）和透平膨胀机（31）的入口相连接，另一根管道（43）将透平膨胀机（31）出口与压缩机（33、36）入口连通，该管作为通道穿过主换热器（17）。
7、如权利要求6所述的装置，其特征是，压缩机（33、36）的出口与主换热器（17）氮通道（39）的出口连通。
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EP0383994A2 (de) 1990-08-29
US5036672A (en) 1991-08-06
EP0384483A2 (de) 1990-08-29
EP0384483B1 (de) 1992-07-22
EP0383994A3 (de) 1990-11-07
AU618659B2 (en) 1992-01-02
JPH02245201A (ja) 1990-10-01

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