CN1096578A - 加压分馏空气生产气态氧和/或气态氮的方法和装置 - Google Patents

加压分馏空气生产气态氧和/或气态氮的方法和装置 Download PDF

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CN1096578A
CN1096578A CN94103958A CN94103958A CN1096578A CN 1096578 A CN1096578 A CN 1096578A CN 94103958 A CN94103958 A CN 94103958A CN 94103958 A CN94103958 A CN 94103958A CN 1096578 A CN1096578 A CN 1096578A
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pressure
fractionation
column
compressed
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B·达雷德奥
C·加尼尔
A·吉尔拉德
P·弗雷斯
J·-Y·莱曼
N·雷斯
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

全部进入的空气被加压到某一高压，然后冷却到 中温。在此温度下，一部分空气膨胀作功到中压，其 余部分被液化。允许在需要时调整生产液态的氧和 /或氮，从双分馏塔排出的补充循环流体被再加热， 压缩到循环的高压，冷却，其中的一部分被压缩的补 充循环流体膨胀，同时对外作功，而其余的则被液 化。

Description

本发明涉及加压生产气态氧和/或气态氮的方法，在该方法中：
-空气在双分馏塔中分馏，该双分馏塔包括一台低压塔（在所谓的低压下操作）和一台中压塔（在所谓的中压下操作）;
-全部待分馏的空气被压缩到至少明显高于中压的高压;
-该压缩空气被冷却到中温，其中的一部分在其被送入中压塔之前在透平机中膨胀到中压;
-未膨胀的空气被液化，在膨胀后被送入双分馏塔;和
-至少一种从双分馏塔排出的液态产品达到生产压力，该液态产品通过在冷却至少一部分待分馏的空气过程中进行热交换而被气化。
本说明书中所论及的压力均为绝对压力。此外，措词“液化”或“冷凝”应在广义上理解，也就是说在超临界压力的情况下包括准液化或准冷凝。
上述的这些步骤在FR-A-2  674  011中作了介绍。
本发明的目的在于，采取经济的方法调整生产，使其既可在加压下生产液体，同时又可生产气体。
为达到此目的，本发明除具有以上列举的步骤外，还具有下列特征，即从双分馏塔排出或直接流向双分馏塔的补充循环流体被加热，压缩到循环的高压，冷却，其中的一部分被压缩的补充循环流体膨胀，对外作功，而其余的则被液化。
根据另外的特征：
-补充的循环流体是中压空气，在其被再加热后与被预压缩到中压的待分馏空气混合，然后将该混合物压缩到所述的高压;
-待分馏的预压缩空气与净化前的再循环空气混合，该混合物被压缩到所述的高压后，在该高压下除去其中的水分和二氧化碳;
-待分馏的预压缩空气在与再循环空气混合之前，其中的水分和二氧化碳被除去;
该循环的补充流体是从两个塔中至少一个塔的顶部排出的氮气，将膨胀的一部分氮气再加热，而液化的部分则再送入双分馏塔或作为产品回收。
本发明为实现其目的，还具有适合于实施这种方法的装置。该装置包括：一组双分馏塔，该塔包括一台低压塔（在所谓的低压下操作）和一台中压塔（在所谓的中压下操作）;压缩设备，可将全部待分馏的空气至少压缩到明显高于中压的高压;用于从双分馏塔排放和泵送至少一种由分馏产生的液态产品的设备;一套热交换系统，用以使所述液态产品在冷却至少一部分待分馏的空气过程中进行热交换;用于使一部分这种空气膨胀的主透平机，该透平机的进口连接到热交换系统的中部，而其出口则连接到中压塔上，其特征在于它包括一台循环压缩机和所述热交换系统包括使从双分馏塔排出的或流向双分馏塔的补充循环流体再加热的管道（连接到循环压缩机的吸入口）、用于压缩补充循环流体的冷却管道（连接到循环压缩机的输出口）和一台用于膨胀一部分补充循环流体的循环透平机，其进口连接到这些冷却管道的中部。
根据该装置的其它特征：
-再加热管道的进口连接到中压塔的底部，而其出口则连接到第二级空气压缩机（构成所述的循环压缩机）的吸入口，所述吸入口也连接到一台空气预压缩机的出口，所述主透平机也构成循环透平机;
-一套通过吸附净化空气的装置，安装在第二级空气压缩机的出口处;
-一套通过吸附净化空气的装置，安装在空气预压缩机和第二级空气压缩机之间;
-再加热管道的进口连接到中压塔的顶部和/或低压塔的顶部，冷却管道的出口则通过膨胀阀连接到双分馏塔上;
-用于预冷却一部分循环氮气的制冷系统，安装在最后一级循环压缩机的出口处。
本发明实施方案的一些实施例将按照图1-3作详细说明，这些示意图分别表示根据本发明的装置的三种实施方案。
示于图1的装置适合于在约3-100巴的高压下生产气态氧、液态氧和液态氮。
该装置主要包括：一台主要的空气预压缩机1或中压压缩机，在其出口处装有空气或水冷制冷器2;第二级主要的空气压缩机3，在其出口处装有空气或水冷制冷器4;在需要时还装有制冷器组5;一套用于通过吸附进行净化的装置6;鼓风机-透平机机组包括一台鼓风机7和一台透平机8，它们的转子固定在同一个转轴上;一套用于鼓风机的空气或水冷制冷器9;一套热交换系统10;一台双分馏塔11，包括一台中压塔12和一台低压塔13，其间由气化器-冷凝器14连接，该气化器-冷凝器用来使塔12顶部的氮气和塔13底部的液态氧进行热交换;一台液氧泵15;一个常压液态氧贮槽16;一个常压液态氮贮槽17;一台分相器18;以及一台过冷器19。
在操作中，塔13处于稍高于1巴的压力下，而塔12则处于相当于约5.5巴的压力下。
全部待分馏的空气在1中被压缩到中压，然后，在3中再压缩，在4和5中预冷却到5-10℃，在6中除去其中的水分和二氧化碳并进一步在7中被压缩到高压。在9中预冷却后，在10中部分冷却到中温T1，一部分高压空气继续在热交换系统中冷却，液化，然后被分成两部分。每一部分分别被膨胀阀20、21膨胀，然后被分别送入塔12、13。
在温度T1下，其余高压空气从热交换系统排出，在8中膨胀作功到中压，然后，被送入塔12的底部。
按照常规的方法，从塔12底部排出的“富液”（富氧空气），和在该塔顶部排出的“贫液”（稍纯的氮气）在19中过冷却和分别在膨胀阀22和23中膨胀后，分别被送入塔13的中部和顶部。
液态氧从塔13的底部排放。一部分直接进入贮槽16，而其余部分用泵15加压到所需的生产高压，然后在通过管线24回收之前气化并在热交换系统中再加热到环境温度。
此外，从塔12顶部排出的处于中压的液态氮，在19中再冷却，在膨胀阀25中膨胀到常压，然后送入分相器18。该液相被送到贮槽17，而气相则与塔13顶部而来的不纯氮气混合，在19然后在10中再加热后，通过管线26作为废气从该装置中排放。
此外，数量约为进入空气量20%的空气，通过管线27从塔12的底部排出，在10中再加热到环境温度，返回到压缩机3的吸入口，并在该处与来自压缩机1的中压空气混合。
这样，压缩机3、制冷器组5、净化装置6和鼓风机7处理进入装置被通过管线27再循环的空气流扩大的空气流，透平机8构成用于进入空气的克劳德循环透平机和再循环空气的循环透平机。可以这样理解，再循环空气一方面通过其在8中膨胀，可以供给生产大量液体所需的冷，而通过其在10中液化又可使液态氧气化。
照这样，通过简单地调整再循环空气的流量，即可按需要改变该装置所生产的液体（液态氧和/或液态氮），而且液体的比能基本上恒定。
作为数量的实例，高压氧可以达40巴，其纯度约为99.5%，压缩机3的出口压力为27巴，另一台压缩机7的出口压力为35巴。
按照一般的方式，氧的高压可以包括在大约3-100巴之间，而在包括大约7-100巴之间的高压下，可以生产类似的气态氮。此外，根据上文引用的FR-A-2  674  011介绍，在温度等于或明显高于空气冷凝的相应温度时，一种或几种液体可以产生气化。同样，通过采用几种高气压，可以生产几种压力的氧和/或氮。
示于图2的装置与图1所示的不同，其差别仅在于制冷器组5和净化装置6系统安装在制冷器2和压缩机3之间。因此，装置6仅处理进入的空气流，而且处于中压，压缩机3处理干燥的和不含二氧化碳的空气。根据该工艺过程的参数进行计算的结果表明，图1和图2的一种或另一种配置可以获得最佳的经济效益。
图3的实施方案中，未标出配件16和19，该再循环流体是氮气，一部分通过管线28从中压塔12的顶部而来，一部分通过管线29从低压塔13的顶部而来，该塔属于“尖塔”型，即是说在其顶部可以生产出几乎纯的氮气。因此，图1中的管线27以及压缩机3和其制冷器4均被省略，而单独由压缩机1将全部进入的空气加压到原来为压缩机3的出口压力。
低压氮在10中再加热，然后通过第一级循环压缩机30（其后是制冷器30A）压缩到中压，与同样在10中再加热的中压氮气混合。这两种中压的氮气流通过第二循环压缩机31（其后是制冷器31A）被压缩到高循环压力。再加热的低压氮气可以通过管线32部分回收作为产品，同样，来自压缩机31的高压氮气可以通过管线33部分回收作为产品。其余从压缩机33而来的氮气进一步通过鼓风机34（其后是制冷器34A，并与膨胀透平机35连接）压缩。经过再压缩的氮气（其中的一部分最好通过制冷器组36预冷却）在10中被冷却到中温T2;在此温度下，一部分从热交换系统排出，在35中膨胀到中压，然后，再送入中压氮气循环的再加热管道。未膨胀的高压氮气继续冷却，而被液化，直到热交换系统的冷端，在膨胀阀37中被膨胀到中压，然后，送入塔12的顶部。
此外，调整用作补充循环流体的氮气流速和高循环压力，可以在宽的范围内改变该装置所生产的液体产品，而且也可以使能耗最佳化。另外，将氮气循环结合到热交换系统10中可以获得只需中等投资的效果。
当然，该整体化的氮气循环可以包括几台并联的膨胀透平机，以便使能量效率最佳化。

Claims (11)

1、一种加压生产气态氧和/或气态氮的方法，在该方法中：
-空气在双分馏塔(11)中分馏，该双分馏塔包括一台低压塔(13)(在所谓的低压下操作)和一台中压塔(12)(在所谓的中压下操作)；
-全部待分馏的空气被压缩(在1、3、7中)到至少明显高于中压的高压；
-该压缩空气被冷却到中温，其中的一部分在其被送入中压塔(12)之前在透平机(8)中膨胀到中压；
-未膨胀的空气被液化，膨胀后(在20、21中)被送入双分馏塔；和
-至少一种从该双分馏塔排出的液态产品达到生产压力，该液态产品通过在冷却至少一部分待分馏的空气过程中进行热交换而被气化，
其特征在于从双分馏塔(11)排出的或流向该塔的补充循环流体被加热，压缩到(在3；30、31中)循环的高压，冷却，其中被压缩的补充循环流体一部分膨胀(在8；35中)，对外作功，而其余的则被液化。
2、根据权利要求1的方法，其特征在于补充的循环流体是中压空气，在其被再加热后与被预压缩到中压（在1中）的待分馏空气混合，然后将该混合物压缩到所述的高压（在3中）。
3、根据权利要求2的方法，其特征在于预压缩（在1中）的待分馏空气与净化前的再循环空气混合，将该混合物压缩到所述的高压，然后，在该高压下（在6中）（图1）将其中的水分和二氧化碳除去。
4、根据权利要求2的方法，其特征在于预压缩（在1中）的待分馏空气在与再循环空气（图2）混合之前（在6中），其中的水分和二氧化碳被除去。
5、根据权利要求1的方法，其特征在于该补充的循环流体是从两个塔（12、13）中至少一个塔的顶部排出的氮气，将膨胀的一部分氮气再加热，液化的部分则再送入双分馏塔或作为产品回收。
6、一套在加压下生产气态氧和/或气态氮的装置，该装置包括：一组双分馏塔（11），该双分馏塔包括一台低压塔（13）（在所谓的低压下操作）和一台中压塔（12）（在所谓的中压下操作）;压缩设备（1、3、7），可将全部待分馏的空气至少压缩到明显高于中压的高压;用于从双分馏塔排放和泵送至少一种由分馏产生的液态产品的设备（15）;一套热交换系统（10），用以使所述液态产品在冷却至少一部分待分馏的空气过程中进行热交换;和用于使一部分这种空气膨胀的主透平机（8），该透平机的进口连接到热交换系统的中部，而其出口则连接到中压塔（12）上，其特征在于它包括一台循环压缩机（3、7;30、31、34），所述热交换系统（10）包括使从双分馏塔（11）排出的或流向该塔的补充循环流体再加热的管道（连接到循环压缩机的吸入口）、用于压缩补充循环流体的冷却管道（连接到循环压缩机的输出口）和一台用于膨胀一部分补充循环流体的循环透平机（8;35），其进口连接到这些冷却管道的中部。
7、根据权利要求6的装置，其特征在于再加热管道的进口连接到中压塔（12）的底部，而其出口则连接到第二级空气压缩机（3）（构成所述的循环压缩机）的吸入口，该吸入口也连接到空气预压缩机（1）的出口，所述主透平机（8）也构成循环透平机。
8、根据权利要求7的装置，其特征在于一套通过吸附净化空气的装置（6），安装在第二级压缩机（3）的出口处。
9、根据权利要求7的装置，其特征在于通过吸附净化空气的装置（6），安装在空气预压缩机（1）和第二级压缩机（3）之间。
10、根据权利要求6的装置，其特征在于再加热管道的进口连接到中压塔（12）的顶部和/或低压塔（13）的顶部，冷却管道的出口则通过膨胀阀（37）连接到该双分馏塔上。
11、根据权利要求10的装置，其特征在于用于预冷却一部分循环氮气的制冷系统（36），安装在最后一级循环压缩机（34）的出口处。
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