CN1080390A - 加压生产气体氧的方法和装置 - Google Patents

加压生产气体氧的方法和装置 Download PDF

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CN1080390A
CN1080390A CN93107602A CN93107602A CN1080390A CN 1080390 A CN1080390 A CN 1080390A CN 93107602 A CN93107602 A CN 93107602A CN 93107602 A CN93107602 A CN 93107602A CN 1080390 A CN1080390 A CN 1080390A
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M·格雷尼尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

进入体系的空气全部被压缩到第一级高压P1， 其中一部分被进一步压缩到压力P2。在中温下，每 一批空气流中的一部分在透平机(7、8)中膨胀。在介 乎P1和中压之间的压力P3下，透平机之一可以有产 品输出，其中分离出的氧大部分以液体形式从低压塔 (13)排出，用泵增压至生产压力并借助空气的冷凝或 假冷凝而在热交换系统(2)中于P1、P2或P3中的任 一压力下气化(图1)。

Description

本发明涉及在一套装置中加压分馏空气生产气体氧的方法。该装置包括一套热交换系统和一组双塔式分馏塔，塔组中包括一个一号塔，系在中压下操作，通常称为中压塔;另一个是二号塔，在低压下操作，通常称为低压塔。从低压塔的底部排出的液体氧，用泵送去与高气压下的压缩空气进行热交换，从而使压缩后的氧气化。
下文中所涉及的压力均为绝对压力。此外，“冷凝”和“气化”的概念要根据所论及的压力是亚临界的还是超临界的来理解是冷凝还是气化，严格地说，是假冷凝还是假气化。
上述的这种方法为“泵压”法，可以省去任何气体氧的压缩机。为使能耗达到允许水平，必须将大流量（约为待气化的氧流量的1.5倍）的空气压缩到足够的压力，使得通过逆流热交换可以将氧液化。要做到这一点，常规的技术需用两台串联的压缩机，其中第二台压缩机只处理一部分适于使液体氧气化的空气，这样就使装置的投资费用明显增加。
本发明目的是提出一种用单段空压机的方法，而且该方法具有 高的综合热力学效果。
本发明这种方法的特征在于：
全部待处理的空气均被压缩到第一级高压P1，此压力明显高于中压;
上述空气的第一部分被冷却到第一级中温T1，在此温度下最初的一部分气流在第一级透平机中膨胀，其余部分则被冷却和液化，经膨胀后引入中压塔;
处于第一级高压P1的其余空气被进一步压缩到第二级高压P2，然后冷却到第2级中温T2，在此温度下，最初的一部分气流在第二级透平机中膨胀，而该空气的其余部分则被冷却和液化，经膨胀后引入中压塔;
如果需要，可将透平机之一的出口压力调节到压力P3（介乎上述第一级高压P1和中压之间）;
至少大部分分离出的氧以液体状态从低压塔排出，用泵压缩到至少第一级气化压力，在此条件下借助空气在上述P1、P2和P3之一的高压下的冷凝作用使其气化，也可以在上述一种或几种压力下借助空气冷凝作用而气化。
按照其余的特征：
选择中温T1和T2，使其中之一介乎约0℃和-60℃之间，另一温度在约-80℃和-130℃之间;
供给热透平机的空气流量约为被处理空气流量的20-30%。
从低压塔排出的另一部分液体氧用泵压缩到至少第二级气化压力，并在上述的一种或几种压力下在热交换系统中气化;
从双塔式分馏塔排出的液体氮用泵压缩到至少氮气化压力，并在上述的一种或几种压力下在热交换系统中气化;
来自第一或第二级透平机的空气至少有一部分在第三级透平机中膨胀到低压，从第三级透平机而来的空气被引入低压塔或引入从该塔上部抽出的尾气中;
上述所有来自第一或第二级透平机的空气均在第三级透平机中膨胀，该空气以及从中压塔底部排出的补充空气基本上处于中压;
空气的进一步压缩采用至少两台串联的鼓风机各与透平机中的一台连接的方法来实现。
本发明另一目的是提出适用于实施本方法所用装置。
按照第一种方式，本发明装置包括：双塔式空气分馏塔，其中包括在低压下操作的塔，通常称为低压塔;以及在中压下操作的塔，通常称为中压塔;用于压缩来自低压塔底部排出的液体氧的泵;将待分馏的空气压缩到明显高于中压的高压的空压设备;使高压空气和压缩的液体氧进行热交换的热交换系统，该装置特征在于，压缩设备包括将所有待分馏空气压缩到明显高于中压的第一级高压P1的压缩机，和将处于第一级高压下的部分空气压缩到第二级压P2的设备，其中包括至少两台串联，并各与膨胀透平机连接的鼓风机 ，其中一台与处于第一级高压P1下的第一级空气透平机连接，另一台与部分进一步压缩空气的第二级透平机相连;热交换系统包括来自透平机的高进口温度空气冷却管道，用于冷却。
按照第二种方式，本发明装置包括：双塔式空气分馏塔，其中包括在低压下操作的塔，称为低压塔，另一以及在中压下操作的塔，称为中压塔;用于压缩从低压塔底部排放的液体氧的泵;压缩设备在明显地高于中压的高气压下供应待分馏空气的压缩装置;使高压空气和压缩的液体氧进行热交换的热交换系统，该装置特征在于，压缩设备包括将所有待分馏空气压缩到明显高于中压的第一级高压的压缩机，将处于第一级高压的部分空气压缩到第二级高压的进一步压缩设备，其中包括至少两台串联并各与膨胀透平机连接的鼓风机，其中一台与处于第一级高压P1下的第一级空气膨胀透平机连接，另一台与部分进一步压缩空气的第二级透平机相连，并且两台透平机中一台的进口温度T1介乎0℃和-60℃之间，而另一台的进口温度T2则介乎-80℃至-130℃之间。
以下参照附图说明本发明的操作实施例说明。
图1为本发明气体氧生产装置示意图。
图2为本发明装置对应的计算所得热交换曲线图。
图3和图4为本发明装置两个其他具体实例示意图。
图1所示的装置适宜于在两种不同的压力下生产气体氧，也可在两种不同的压力下生产气体氮，此外还可生产液体氧和液体氮。
该装置主要包括双塔式分馏塔1，热交换系统2，主要的空气压缩机3，出口装有冷却器6的两台串联的鼓风机4、5，“热”透平机7，“冷”透平机8，两台液氧泵9、10以及液氮泵11。
双分馏塔1包括在5-6巴压力下操作的中压塔，在稍稍高于大气压下操作的“尖塔”型低压塔13，将塔12的顶端的气化气（氮）与塔13底部的液体（氧）进行热交换的气化-冷凝器14，与塔13相连的辅助氩生产塔15。
该装置还有常规的管道，包括将塔12底部的“富液”（富含氧的空气）提升到塔15中部和/或提升到塔15的顶部冷凝器的管道16，将塔12中部的“下贫液”（不纯氮）提升到塔13中部的管道17，将塔12顶部的“上贫液”（纯氮）提升到塔13的顶部的管道18，管道16、17和18都安装膨胀阀。通过上述三根管线输送的液体在热交换系统2的冷却段被过冷却。管道18的支管19通向液氮贮罐20，在该支管上装有膨胀阀。
鼓风机4的叶轮与透平机8的叶轮牢固地联结且鼓风机5的叶轮与透平机7的叶轮同样牢固地联结。
在操作中，待分馏空气通过压缩机3全部压缩到约为25-35巴的力P1，并在吸附器21中除去水分和二氧化碳后被分为两股气流。
第一股气流在压力P1下被冷却到中温T1（介乎0℃和-60℃之间）。上述第一股气流中的一部分经过冷却后被液化，然后在膨胀阀 中膨胀到中压，通过管道22送到塔12。上述第一股气流的其余部分在温度T1下从热交换系统中排出，在透平机7中膨胀到中压，重新引入热交换系统，冷却并液化后通过管道23送到塔12。
离开吸附器21的其余空气通过鼓风机4和5进一步两级压缩到压力P2，约为35-50巴，在冷却器6中预冷却，然后在热交换系统中冷却到明显低于T1的第二级中温度T2，介乎-80℃和-130℃之间。上述空气中的一部分经过冷却后液化，然后在膨胀阀中膨胀到中压，并通过上述管道22引进塔12中。压力P2下的其余空气在温度T2下从热交换系统中排出，在透平机8中膨胀到中压，然后通过上述管道23引进塔12中。
在热交换系统2中，空气的冷却是通过几种流体的逆流循环实现的;
来自塔13顶部的低压气体氮和由同一塔产生的不纯或“废”氮，这两种气流通过热交换器，从其冷端到热端，然后通过相应的管道24和25抽出;
经过分离的氧中绝大部分以液体形式从塔13的底部排出，通过泵9使其压力达到较低的第一级压力P01，在压力P1下（相当于P01＝11-17巴）或压力P2下（相当于P01＝17-22巴）借助空气的冷凝作用而使其气化，在室温下再加热后通过管道26作为产品输出;
另一部分经过分离的氧（本实施例要求在较高的第二级压力 P02（一般介乎11和60巴之间）以气相生产）从塔13底部以液体形式排出，使其压力升高到上述第二级压力P02，利用从空气中汲取热量而在热交换系统中气化，这种气化不必伴随，上述空气的冷凝，然后再加热到室温并通过管道27作为产品抽出;和
氮（本实施例要求在约5-60巴，优选约25-35巴的压力下以气相生产）从塔12的顶部以液体形式排出，用泵11将其增压到上述的生产压力，利用从空气中释放出的热量使其气化（这种气化不必伴随上述空气的冷凝），然后再加热到室温并通过管道28作为产品抽出。
本装置在生产气体氧和氮的同时，还生产出大量的液体（氧和/或氮）。对于压缩机3出口处压力为25巴的空气而言，液体的产出量可能达到经过分离的氧流量的40%。图1表明，除用于液体氮的管道19以外，管道29用于生产液体氧。
图2所示的热交换曲线图对应于上述图1，其中有关数据如下：
被处理空气的流率：26，000N米3/小时，
P1＝27.5巴，P2＝39.5巴，
T1＝-35℃，T2＝-122℃.
气体氧生产过程中三分之二在12巴压力（管道26），三分之一在42巴压力（管道27）下进行。
本装置也可在42巴（管道28）下生产1，600N米3/小时的纯 气体氮和1，900N米3/小时的液体氮。
热交换曲线图中曲线C1对应于再加热流体系统，而曲线C2则对应于冷却过程中被处理空气。
从曲线C1上可以看出，A处氧气化段压力12巴，B处拐点对应于42巴压力下氮假气化段，而C处氧的气化段压力42巴（短于A，因为其流量小）。
曲线C2上D点表示空气进口，其压力为P2，温度32℃，E点表示在压力P1及12℃下吸入空气，此处曲线C2和C1之间的温度间隔达到最小值（2℃），这很有利。F点对应于透平机7进口，其斜率低，C段附近的G点表示透平机8进口，该点也获得类似结果，H表示压力P2下空气的假冷凝段，此段位于B假冷凝段附近，而I表示在压力P1下空气的冷凝拐点，该点与A段相对应，与其温度间隔最小，长度与A段相同。
从图2可以看出，在热交换系统所包含的整个温度范围内两条曲线彼此非常接近，表示本方法具有较高的综合热力学效果。
如图1中的虚线所示，作为一种改进，该装置可包括第三透平机30，如由交流发电机31制动，适宜于使一部分来自透平机7的中压空气膨胀到低压状态。如图所示，透平机30的出口与塔13中部相连的或与输送残余不纯氮的管道相连。透平机30的进口温度约为-100℃--150℃。
这样的低压透平机在两种情况下很有用：当所生产的氧的纯度 在85%和98%之间时，一方面可以增加液体的产量而同时又不致明显降低氧的提取产量以稳定低分离能，另一方面，在不利于氧产量情况下，增加液体的产量。如上所述，如果该装置生产氩，则最好将低压空气送入不纯的氮中以保持氩的提取产量，相反可将该低压空气鼓入塔13。
图3所示的装置在下列几方面区别于前述装置：
低压透平机30靠第三台鼓风机制动，后者的叶轮与透平机叶轮牢固联结，并与鼓风机4和5串联安装，位置在后者上游;
在透平机30中膨胀的气体流量比在透平机7中膨胀的流量大。因此，透平机30一方面靠来自透平机7的全部中压空气供料，另一方面，靠通过管道33而来自塔12的中压空气补充，并在热交换系统中再加热到适宜的温度;
只有泵9与氧有关，因此是在单一压力下生产并在三种可达到的压力（P1、P2和中压）之一下借助空气的冷凝而全部气化，而泵10和11则与氮有关，氮气在两种不同的压力下生产并同样借助空气冷凝而气化。
图4所示的示意图与图1的不同之处仅在于透平机7和8的安排上，其中供给“热”透平机7中供入高压P2的空气，而“冷”透平机8中供入压力P1的空气。此外，透平机7是在高于中压的压力P3下输出，其压力实际上是介乎中压和压力P1之间。借助氧气化，压力P3下的空气在热交换系统中冷却并液化，在送到塔12之 前，在膨胀阀34中膨胀到中压。这种安排对于氧的压力在3巴和8巴之间的情况特别有效。
在上述的每个实施例中，本装置的热交换系统2具有三种不同压力的空气冷却管道，可以利用上述的一种或几种压力并在约为2℃的低温差下逆流气化至少大部分离后的氧而使空气冷凝（相应压力下氧含于液相并在该压力下气化），也可在另一压力下的补充氧和/或氮气化而使空气冷凝，必要时氧和/或含于液相并在热交换系统2中气化）。
由于压力P1和P3可以按要求选择，而压力P2可通过选择送入透平机进行膨胀的空气流和压力P1来调节，因此在选择氧的气化压力和必要时选择氮的气化压力时具有很大的灵活性。当在压力P3下大量气化氧而冷凝空气时，该空气的流量可以调节到待气化氧流量，即空气流量调节在待处理的空气流量的20-30%之间，“热”透平机7的这种空气流量可使热力学性能保持最佳水平。
需要注意的是，由于氧和氮比例较小，所以其气化压力不必完全与压力P1、P2和P3关联。
此外，该装置可以生产一部分液体氧和氮，由于在完全不同的进口温度下利用两台膨胀透平机，因而能耗比最佳。

Claims (15)

1、在包括热交换系统(2)和双塔式分馏塔(1)的装置中加压分馏空气生产气体氧的方法，而分馏塔中包括在中压下操作的一号塔(12)，即所谓中压塔，以及在低压下操作的二号塔(13)，即所谓低压塔，其中从低压塔底部排出的液体氧用泵(9，10)加压后与高压压缩空气进行热交换而气化，其特征在于：
全部待处理空气被压缩到明显高于中压的第一级高压P1；
上述空气的第一部分被冷却到第一级中温T1，在此温度下最初的一部分在第一级透平机(7，8)中膨胀，其余部分则被冷却和液化，并膨胀后引入中压塔(12)；
处于第一级高压P1的其余空气被进一步压缩到第二级高压P2后冷却到第二级中温T2，在此温度下最初的一部分气流在第二级透平机(8，7)中膨胀，其余部分则被冷却和液化并膨胀后引入中压塔(12)；
必要时将透平机(7，8)中的一台的出口压力调节到压力P3(介乎上述第一级高压P1和中压之间)；
至少大部分分离出的氧以液体状态从低压塔(13)排出，用泵压缩到至少第一级气化压力，在此压力下借助空气在上述P1、P2和P3之一高压下的冷凝而气化，也可在上述压力或几种压力下借助空气冷凝而气化。
2、按照权利要求1的方法，其特征在于选择中温T1和T2，使其之一为约0℃和-60℃之间，另一温度约-80℃和-130℃之间。
3、按照权利要求1或2的方法，其特征在于供给热透平机（7，8）的空气流量约为被处理空气流量的约20-30%。
4、按照权利要求1-3中任一项的方法，其特征在于从低压塔（13）排出的另一部分液氧用泵压缩到至少第二级气化压力并在上述的一种或几种压力下在热交换系统（2）中气化。
5、按照权利要求1-4中任一项的方法，其特征在于从双塔式分馏塔（1）排出液氮，用泵（10，11）压缩到至少氮气化压力。并在上述的一种或几种压力下在热交换系统（2）中气化。
6、按照权利要求1-5中任一项的方法，其特征在于来自第一或第二级透平机（7，8）的至少一部分空气在第三级透平机（30）中膨胀至低压，从第三级透平机而来的空气被引入低压塔（13）或引入从该塔上部抽出的尾气中。
7、根据权利要求6的方法，其特征在于上述所有来自第一或第二级透平机（7，8）的空气均在第三级透平机（30）中膨胀，该空气基本上处于中压并从中压塔（12）底部排出补充空气。
8、按照权利要求1-7中任一项的方法，其特征在于空气的进一步压缩采用至少两台串联鼓风机（4，5，32）并各与透平机（7，8，30）之一连接的方法来实现。
9、实施权利要求1-8中任一项的方法而加压生产气体氧的装置，其中包括双塔式空气分馏塔（1），该塔又包括在低压下操作的塔，通常称为低压塔（13），以及在中压下操作的塔，通常称为中压塔（12），用于压缩来自低压塔（13）底部排出的液氧的泵（9，10），将待分馏空气压缩到明显高于中压的高压的压缩设备（3，4，5，32），使高压空气和压缩液氧进行热交换的热交换系统（2），该装置特征在于压缩设备包括将所有待分馏空气压缩到明显高于中压的第一级高压P1的压缩机（3），进一步将处于第一级高压的部分空气压缩到第二级高压P2的设备（4，5，32），这些进一步压缩设备包括至少两台各与膨胀透平机（7，8，30）连接的串联鼓风机，其中之一（4，5）与在第一级高压P1下膨胀空气的透平机（7，8）连接，另一台（5，4）与膨胀进一步压缩后的一部分空气的第二级透平机（8，7）相连，热交换系统（2）包括冷却来自透平机（7）的空气的高进口温度冷却管道。
10、按照权利要求9的装置，其特征在于在两台透平机之一（7）的进口温度T1介乎约0℃和-60℃之间，而另一台（8）的进口温度T2则介乎约-80℃和-130℃之间。
11、按照权利要求9或10的装置，其特征在于其中包括用于液氧或液氮泵（10），以及必要时的用于液氧或液氮三级泵（11），而且热交换系统（2）包括与气化－再加热对应管道。
12、根据权利要求9-11中任一项的装置，其特征在于其中包括三级泵（30），将来自透平机（7）的至少一部分空气膨胀到低压的高进口温度三级透平机（30）以及将空气从三级透平机引入低压塔（13）或从该塔引入尾气管道的设备。
13、按照权利要求12的装置，其特征在于其中包括用中压塔（12）底部排出的空气完成第三级透平机（30）供料的设备（33），来自高进口温度透平机（7）的空气基本上处于中压。
14、实施权利要求1-8中任一项的方法而加压生产气体氧的装置，其中包括双塔式空气分馏塔（1），该塔又包括在低压下操作的塔，通常称为低压塔（13），以及在中压下操作的塔，通常称为中压塔（12），用于压缩来自低压塔（13）底部排出的液氧的泵（9，10），将待分馏空气压缩到明显高于中压的高压的压缩设备（3，4，5，32），使高压空气和压缩液氧进行热交换的热交换系统（2），该装置特征在于压缩设备包括将所有待分馏空气压缩到明显高于中压的第一级压力P1的压缩机（3），进一步将处于第一级高压的部分空气压缩到第二级高压P2的设备（4，5，32），这些进一步压缩设备包括至少两台各与膨胀透平机（7，8，32）连接的串联鼓风机，其中之一（4，5）与在第一级高压P1下膨胀空气的透平机（7，8）相连，另一台（5，4）与膨胀进一步压缩后的一部分空气的第二级透平机（8，7）相连，两台透平机之一（7）的进口温度T1介乎约0℃和-60℃之间，另一台（8）的进口温度T2则介乎约-80℃和-130℃之间。
15、按照权利要求14的装置，其特征在于热交换系统（2）包括冷却来自透平机（7）的空气的高进口温度冷却管道。
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