CN1069329A - 精馏分离空气的方法和设备 - Google Patents

精馏分离空气的方法和设备 Download PDF

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CN1069329A
CN1069329A CN92109305A CN92109305A CN1069329A CN 1069329 A CN1069329 A CN 1069329A CN 92109305 A CN92109305 A CN 92109305A CN 92109305 A CN92109305 A CN 92109305A CN 1069329 A CN1069329 A CN 1069329A
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crude argon
column
argon
medium pressure
oxygen
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迪特里希·罗特曼
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Linde GmbH
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Abstract

本发明描述了一种用两级精馏塔分离空气随后 再制取粗氩的方法，使从粗氩塔(20)中抽取的粗氩流 (25，31)的一部分同中压塔(4)中抽出的液态氧产品 流(40)进行间接热交换而冷凝，同时部分氧产品流 (40)蒸发。然后将冷凝的粗氩(35)再送回到粗氩塔 (20)中，提取粗氩的第二部分作为产品(24)。

Description

本发明涉及一种精馏分离空气的方法及实施该方法的设备。在本发明的方法中，空气经压缩、净化、冷却、然后在两级精馏塔的高压塔中被粗分馏成富氧液体及富氮馏分，至少将部分富氧液体和/或富氮馏分送入精馏塔的中压塔中并分离成氧气和氮气，从中压塔中抽取含氩的氧流和氧产品流，同时将含氩的氧流送入粗氩塔中，粗氩塔的工作压力低于中压塔的工作压力，从粗氩塔的上部提取氩气。
在DE-A-3905521中公开了这种在空气分离之后制取粗氩的方法。
在该方法中，粗氩精馏是在压力低于两级精馏塔的中压塔工作压力的条件下进行的。使从中压塔流出的含氩的氧流在进入粗氩塔之前膨胀作功。从高压塔塔釜处抽出大部分可以应用的富氧液体。在粗氩塔的顶部冷凝器中，使气态粗氩与来自高压塔的已膨胀的富氧液体进行间接热交换而液化，蒸发的富氧馏分经压缩而被送入中压塔内。
现有的方法是通过装在分离具有一定压力的氧或具有一定压力的氮的空分塔下游、工作压力低于中压塔压力的粗氩塔来制取氩的，虽然在制取氩的过程中氩产量的损失不太大，但是仍存在不足之处，特别是为了冷却粗氩塔需要膨胀和再压缩富氧馏分，所需费用是极其昂贵的。此外，由于进入中压塔的富氧馏分的蒸发部分为气态，不能再用作回流液，因此，中压塔中的精馏工况尤其是氩产量不能令人满意。
本发明的任务是要改进上面所提到的方法，以便能经济而高效地制取氩。
完成上述任务的技术方案是：从中压塔中引出液态氧产品流，使从粗氩塔中抽取的粗氩中的至少一部分粗氩与液态氧产品流进行间接热交换而冷凝，在上述热交换过程中至少部分氧产品流被蒸发，同时将冷凝的粗氩再送回粗氩塔中。
与现有的方法相比，本发明的方法具有很多优点：可以使从高压塔引出的全部富氧馏分在较高的位置流入中压塔;回流比F/D趋于1;还可避免气态馏分的影响。
因此，本发明的方法大大改善了中压塔中的精馏工况，这说明在理论塔板数不变的情况下可提高产量，尤其可提高氩的产量。而且还能用上述馏分中的一种-即从中压塔引出的氧产品经济地冷却粗氩塔。
如果在液态氧产品流与冷凝的粗氩进行间接热交换之前提高液态氧产品流的压力，本发明的方法还具有另外的优点。虽然，为了经济地制取高压氧，先使氧气在一定压力下液化，然后再使其蒸发，这种步骤已是公知的，但通常是压缩与冷凝的输入空气逆向流动的氧，随后将上述冷凝的输入空气送入高压塔中，这种液态输入空气对高压塔中的精馏过程会产生不良影响。
按照本发明的方法在制取具有一定压力的氧时不会影响精馏过程，反之，使具有一定压力的液态氧与某种期望液化的馏分逆向流动而蒸发，同时将上述已液化的馏分用作回流送入粗氩塔中。
提高液态氧的压力的方法例如可采用泵或利用中压塔和氧蒸发器之间的流体静力势能。
事实证明，如果按照本发明的方法使粗氩在同液氧产品流进行间接热交换之前复热、压缩和冷却也是很有利的。
可以采用一级或多级压缩粗氩，通过一台或几台压缩机可将粗氩压缩到所期望的压力，最终可使粗氩的压力达到蒸发的氧产品流的压力水平。因此，输出的氧的压力在很宽的范围内不会产生其它方法中所存在的重要的负作用。
最好使冷凝的粗氩在与液态氧产品流间接热交换之后过冷并使其在进入粗氩塔之前膨胀。若将冷凝的粗氩与从粗氩塔中提取的粗氩进行间接热交换来实现上述过冷则更为有效。
在本发明的另一实施方案中，使从中压塔中抽出的含氩氧气流在进入粗氩塔之前膨胀作功，并至少将作功膨胀所得到的功的一部分用于压缩粗氩，因而大大降低了用来压缩与蒸发的氧气反向并朝上流动的冷凝粗氩所需的外加能量的消耗。
本发明的另一个改变是将蒸发的氧产品流的一部分送入中压塔的下部，因此，在中压塔中，粗氩的冷凝作用会形成附加的向上升的气体，从而强化了主冷凝器的效果。
最好将从粗氩塔中抽取的粗氩的一部分作为产品。
附图说明：
图1为本发明方法的一种实施方案的示意图。
下面将结合附图对本发明及本发明其它内容进行详细描述。
经压缩及预净化的空气由管道1引入，在热交换器36中与产品流进行间接热交换而被冷却，然后被送入两级精馏塔的高压塔3中。用一个公用的冷凝器/蒸发器13使高压塔3（工作压力为6至20巴，最好为8至17巴）与中压塔4（工作压力为1.5巴-10巴，最好为2.0-8巴）相连，并使二者进行热交换。输入的空气在高压塔中被粗分馏成氮气和富氧馏分。高压塔塔釜中的液态富氧馏分经管道6流出，在热交换器32中过冷，再经阀门10节流而进入中压塔4中。高压塔3顶部的氮同样以液态的形式经管道5抽出，再在热交换器32中过冷，一部分作为液态产品经管道8抽出，从高压塔3引出的另一部分氮作为回流经管道9送入中压塔4中。
抽取液态氧（经管道40）、气态纯氮（经管道15）以及不纯的氮气（经管道16）作为中压塔的产品，并使上述两股氮馏分经热交换器32和36而复热。
对该过程而言，如果透平膨胀机18所产生的冷量不够的话，由于中压塔4中的压力较高，用管道16中的不纯的氮气来补偿过程中不足的冷量也是合适的。但是附图中却没有示意地将为此而必备的步骤表示出来。
除上述已提到的物流外，从中压塔4经管道17还抽出一股含氩的氧流，使该氧流经热交换器36复热，再送入粗氩塔20中，粗氩塔的工作压力为1.1-2巴，最好是1.3-1.5巴。在粗氩塔20的贮槽中附带产生的其余馏分经管道22抽出，并经泵23增压至反送到中压塔4中所需的压力。此外，还使富含氩的氧流17在进入粗氩塔20之前经透平膨胀机18作功膨胀，以使富含氩的氧流一方面减到粗氩塔20所存在的低压，另一方面提供工艺中所需的冷量。
将在粗氩塔20顶部产生的气态粗氩经管道21抽出，送入热交换器37中使其与冷却的冷凝粗氩进行逆向热交换而复热，然后经热交换器36被再加热，最后分成两部分物流24和25引出。将经管道24输出的粗氩气流作为中间产品从设备中抽出并提供给用户，而由管道25引出的粗氩气流不从设备中抽出，使其经两级压缩机26和29压缩，每级压缩之后都要进行冷却（由水冷却器28和30冷却），然后，使此股粗氩气流经管道31通过热交换器36而进一步冷却，最后将其送入安装在冷凝蒸发器33中的冷凝器34中。在冷凝器34中，该股粗氩由经管道40并由泵41泵入的逆向流动的液态氧冷凝。接着，将已冷凝的粗氩经管道35送入热交换器37中，在该热交换器中使其被从粗氩塔20中抽出的逆向流动的粗氩冷却，然后经阀38节流膨胀后进入粗氩塔20。
经管道40并由泵41泵入冷凝蒸发器33中的具有一定压力的液态氧产品流与经管道31流入的粗氩流的一部分进行间接热交换而被部分蒸发。使氧产品流的此部分蒸汽状的馏分经管道42在热交换器36中复热后流出。不需要作为产品输出的部分气态氧产品流可由管道43引出，经阀44膨胀后再送入中压塔的贮槽中。通过管道45可从冷凝蒸发器33中抽取液态氧产品流。
图中虚线所表示的工艺流程补充描述了氮的附加循环。
将从管道15流出的氮馏分的一部分由管道50抽出，送入压机51中压缩，然后由水冷却器52冷却，再经管道53进入热交换器36中过冷后送入装在高压塔3的塔釜中的加热盘管54中，由此而形成的氮冷凝液经管道55及阀门56引入高压塔的上部区域、液态氮（经管道5输出）抽料口的上方或下方（为清楚起见，图中氮冷凝液进入高压塔的入口位置在液态氮抽料口的下方）。这种节流后送入高压塔上部区域的氮冷凝液对从中压塔抽取氩而言所起的作用是积极的，因为通过加入附加的氮改善了中压塔的回流比。
此外，采用塔釜加热器54使所需的空气量大大减少，致使在不纯的氮气中任意低的氧纯度都可识别出来。
在空分设备与发电设备（例如GUD发电设备）或其它具有燃气轮机的设备（例如生产钢的设备）联成一体时采用本发明的方法尤其有利。
此外，在一个塔或几个塔或每一个塔（高压塔、低压塔、粗氩塔）中充填无序填料或有序填料也是有利的。当其它区域例如底部有填料时，也可以在塔的部分区域装填填料。

Claims (17)

1、一种精馏分离空气的方法，在该方法中空气(1)经压缩、净化、冷却(36)，然后在两级精馏塔(2)的高压塔(3)中被粗分馏成富氧液体(6)和富氮馏分(5)，至少将一部分富氧液体(6)和/或富氮馏分(5)送入上述精馏塔(2)的中压塔(4)中，从而分离出氧气和氮气，从中压塔(4)中抽取含氩的氧流(17)和氧产品流(40)，同时将含氩的氧流送入粗氩塔(20)中，上述粗氩塔的工作压力低于中压塔(4)的工作压力，然后从粗氩塔的上部区域提取粗氩(21)，其特征在于从中压塔(4)中所提取的氧产品流(40)为液态，至少使从粗氩塔(20)抽取的粗氩的一部分(31)与上述液态氧产品流(40)进行间接热交换(在(34)中进行)而冷凝，与此同时，至少使氧产品流(40)的一部分蒸发，然后将冷凝的粗氩(35)再送回到粗氩塔(20)中。
2、如权利要求1所述的方法，其特征在于使液态氧产品流（40）在与冷凝的粗氩进行间接热交换（在（33、34）中进行）之前增压。
3、如权利要求1或2所述的方法，其特征在于使粗氩（25）在与液态氧产品流进行间接热交换（在（34）中进行）之前复热（在热交换器（37）中进行）、压缩（用压缩机（26，29）实现）。和冷却（通过水冷却器（28，30），及热交换器（36）实现）。
4、如权利要求1-3中任一项所述的方法，其特征在于使上述冷凝的粗氩（35）在与液态氧产品流进行间接热交换（在（34）中进行）之后过冷（在热交换器（37）中进行），然后使其在进入粗氩塔（20）之前膨胀（由膨胀机（38）实现）。
5、如权利要求4所述的方法，其特征在于上述冷凝的粗氩（35）的过冷却是通过与从粗氩塔（20）中提取的粗氩进行间接热交换（在热交换器37中进行）来实现的。
6、如权利要求3-5中任一项所述的方法，其特征在于使从中压塔（4）中流出的含氩的氧流（17）在进入粗氩塔（20）之前作功膨胀，而将至少一部分作功膨胀过程中所获得的功用于压缩（经压缩机29）粗氩（25）。
7、如权利要求1-6中任一项所述的方法，其特征在于将一部分蒸发的氧产品流送入（用管道43）中压塔的下部。
8、如权利要求1-7中任一项所述的方法，其特征在于从粗氩塔（20）中提取粗氩（21）的一部分作为产品（24）。
9、实现权利要求1-8中所述方法的设备包括具有高压塔（3）和中压塔（4）的精馏塔（2）;一根将经压缩净化和冷却的空气送入高压塔中的进料管道（1）;至少一根连接高压塔（3）和中压塔（4）的连接管道（5，6）;从中压塔（4）经减压装置（18）通到粗氩塔（20）的氩输送管道（17，19），同粗氩塔（20）的上部相通的粗氩输出管道（21，31），其特征在于还包括一个冷凝蒸发器（33，34），该冷凝蒸发器的冷凝侧（34）经粗氩输出管道（21，25，31）和粗氩冷凝管道（35）与粗氩塔（20）相通，冷凝蒸发器的蒸发侧经液体输送管（40）与中压塔（4）的下部区域相通。
10、如权利要求9所述的设备，其特征在于还包括一个设置在液体输送管路（40）上的泵（41）。
11、如权利要求9或10所述的设备，其特征在于上述冷凝蒸发器（33，34）的位置低于中压塔（4）。
12、如权利要求9-11中任一项所述的设备，其特征在于在粗氩输出管路（25）上装有压缩装置（26，29）。
13、如权利要求9-12中任一项所述的设备，其特征在于还包括一个粗氩过冷却器（37），其热流通道与粗氩冷凝管道（35）相通。
14、如权利要求13所述的设备，其特征在于上述粗氩过冷却器（37）的冷流通道与粗氩输出管道（21）相通。
15、如权利要求9-14中任一项所述的设备，其特征在于上述减压装置（18）有一个膨胀机，该膨胀机安装在氩输送管路（17，19）上。
16、如权利要求12和15所述的设备，其特征在于上述压缩装置至少有一台压缩机，该压缩机与上述膨胀机（18）机械耦联。
17、如权利要求9-16中任一项所述的设备，其特征在于还包括一根蒸汽管道（43），该管道从冷凝蒸发器的蒸发侧通到中压塔（4）的下部区域。
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AU2099392A (en) 1993-02-18
US5251449A (en) 1993-10-12
EP0527501A1 (de) 1993-02-17
CA2075737A1 (en) 1993-02-15

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