CN1057380C - 低温空气分离方法和设备 - Google Patents

低温空气分离方法和设备 Download PDF

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CN1057380C
CN1057380C CN91105298A CN91105298A CN1057380C CN 1057380 C CN1057380 C CN 1057380C CN 91105298 A CN91105298 A CN 91105298A CN 91105298 A CN91105298 A CN 91105298A CN 1057380 C CN1057380 C CN 1057380C
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J·R·德雷
D·R·帕斯尼克
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Union Carbide Industrial Gases Technology Corp
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Abstract

本发明公开了一种包括至少两个塔的空分***，该***中，两部分原料空气在两种不同温度下透平膨胀，以产生冷量，原料空气的第三部分与从该空分设备中取出的正蒸发的产品进行热交换而被冷凝，这三部分原料空气全都送入同一塔中，以进行分离。

Description

低温空气分离方法和设备
本发明一般地涉及低温空气分离领域，更具体地说，涉及从空气分离中生产高压气体产品，也可从该空气分离中获得液体产品。
常用于空气分离的工业***是低温精馏，它是利用高进气压来进行分离的，这种高进气压通常是将原料空气在引入塔***之前经压缩机压缩而获得的。进行空分时，液体和蒸气逆流接触通过该塔或几个塔的汽-液接触部件，使易挥发组份从液体变成蒸汽，而不易挥发组份由蒸汽变成液体。蒸汽在塔内上升的过程中，易挥发组份逐渐增多，液体在塔内下降的过程中，不易挥发的组份逐渐增多。通常低温分离是在主塔***和辅助氩塔中进行的，主塔***至少包括一个塔，在该塔中原料空气被分离成富氮组分和富氧组分，从主塔***中流出的原料空气在辅助氩塔中被分离成富氩组分和富氧组分。
人们常常希望从空气分离***中回收到高压气体产品。通常是用压缩机将产品气体压缩到高压，这种***很有效，但十分昂贵。在某些情况下，还需要生产液体产品，所生产的液体产品可用于长时间需要的情况，以及不使用气体产品的场合。
因此，本发明的目的是要提供一种改进的低温空气分离***。
本发明的另一个目的是要提供一种用于生产高压产品气体而又减少或不需要对产品气体进行压缩的低温空气分离***。
本发明还有一个目的是要提供一种用于生产高压气体产品同时还生产液体产品的空气分离***。
本领域的普通专业技术人员阅读了本发明所公开的内容后，将能清楚地看到用本发明可达到上述目的及其它目的。本发明一般包括将不同温度的、压缩过的两部分原料空气进行透平膨胀，以向设备供冷；冷凝另一部分与正蒸发的液体进行热交换的原料空气，以生产气体产品。
更具体地说，本发明一方面包括：
利用低温精馏分离空气以生产气体产品的方法，它包括如下步骤：
(A)透平膨胀经压缩的原料空气的第一部分，冷却经透平膨胀的第一部分气体，将所生成的冷却、透平膨胀过的第一部分空气送入空分设备的第一塔，第一塔的运行压力范围一般为413685.60-689476帕；
(B)冷却压缩过的原料空气的第二部分，将已冷却的第二部分在低于步骤(A)中透平膨胀温度的温度下进行透平膨胀，将所生成的经透平膨胀的第二部分空气引入第一塔；
(C)至少部分冷凝原料空气的第三部分，将所生成的液体引入第一塔；
(D)将流入第一塔的流体分离成富氮和富氧流体，并将此两股流体引入空分设备的第二塔，第二塔的运行压力低于第一塔；
(E)将流入第二塔的流体分离成富氮蒸汽和富氧液体；
(F)通过与原料空气的第三部分进行间接热交换来蒸发富氧液体，以进行步骤(C)中的冷凝；
(G)回收经步骤(F)中热交换而生成的蒸汽，以当作氧气产品。
本发明另一方面包括：
利用低温精馏分离空气以生产气体产品的设备，它包括：
(A)一个空气分离设备，包括：
一个第一塔、一个第二塔、一个再沸器、将流体从第一塔送到再沸器的装置、及将流体从再沸器送到第二塔的装置；
(B)一个第一透平膨胀机、向第一透平膨胀机供给原料空气的装置、将流体从第一透平膨胀机送到热交换器的装置，及将流体从热交换器送到第一塔的装置；
(C)一个第二透平膨胀机、冷却原料空气并将冷却过的原料空气送至第二透平膨胀机的装置，以及将流体从第二透平膨胀机送至第一塔的装置；
(D)一个冷凝器、向该冷凝器供给原料空气的装置、及将流体从冷凝器送至第一塔的装置；
(E)将流体从空分装置送入上述冷凝器的装置，以及
(F)从该冷凝器中回收产品气体的装置。
此处所使用的术语“塔”指的是一种蒸馏或精馏塔、或蒸馏或精馏区，即一种接触塔或区域，在该塔或区中液相和汽相逆流接触，以实现流体混合物的分离。例如，汽相和液相可以在安装在塔内的一系列垂直相隔的盘或板上接触，或者也可以在填料部件上接触。对于蒸馏塔的进一步讨论可以参见“化学工程手册”(第5版，由R.H.Perry和C.H.Chilton编，McGraw-Hill图书公司出版、纽约)的第13章，即“蒸馏”一章的第13-3页上B.D.Smith等人的文章“连续蒸馏过程”(The Continuous Distillation Process)。术语“双级塔”指的是一种高压塔，其上端与低压塔的下端处于热交换关系。关于双级塔的进一步讨论发表在Ruheman的“气体分离(The Separation ofGases)”一书(牛津大学出版，1949年)的第7章“工业空气分离(Commerical Air Separation)”中。
术语“氩塔”指的是一种塔，在该塔中通过往上流的蒸汽与向下流的液体逆向流动，使上流的蒸汽中氩的含量逐渐增多，氩气产品从该塔中抽出。
术语“间接热交换”的含义是：两种流体进行热交换时没有任何直接接触，或者流体之间互不掺混。
术语“汽-液接触部件”是指在两相逆流流动期间，在液汽接触界面处任何有助于传质或有助于组分分离的塔内部件。
术语“塔盘”指的是一种大体上是平坦的板，板上有孔、液体入口和出口，液体能流过板，而蒸汽通过孔上升，以便两相之间进行传质。
术语“填料”的含义是指用作塔内部件的任何具有予定结构、尺寸和形状的实体或空心体，它们为液体提供了表面积，从而能在两相逆流流动期间，在液-汽接触界面处进行传质。
术语“无规填料”意指各个填料互相之间或相对于塔轴线来说无特定取向的填料。
术语“结构定形填料(structured packing)”指的是各个填料彼此之间、以及相对于塔轴线而言具有特定取向的填料。
术语“理论段”的含义是指在某段中向上流动的蒸汽和向下流动的液体之间为理想接触，使离开的流体保持在平衡状态。
术语“透平膨胀”意指让高压气流通过一个透平机而降低该气体的压力和温度，从而产生冷量。一般常采用负载装置，如发电机、功率计或压缩机之类来回收能量。
术语“冷凝器”是指一种靠间接热交换的方式冷凝蒸汽的热交换器。
术语“再沸器”意指一种靠间接热交换的方式蒸发液体的热交换器。再沸器一般用在精馏塔的底部，以向汽-液接触部件提供蒸汽流。
术语“空气分离设备”指的是一种利用低温精馏的方法分离空气的设备，它包括至少一个塔和附属连接装置，如泵、管路、阀和热交换器等。
图1是本发明的低温空气分离***的一个最佳实施例的流程简化示意图；
图2是空气冷凝压力与氧沸腾压力的关系曲线图。
下面将参照附图详细描述本发明。
参见图1，原料空气100通常被压缩到绝对压力为620528.40-3447380帕(绝对压力)的范围内，然后与流过热交换器101的逆向回流进行间接热交换而被冷却。经压缩的原料空气的第一部分200在完全流过热交换器101之前中途从热交换器101中抽出，并被送入第一透平膨胀机201中，在该膨胀机中，气流通常被膨胀到压力为413685.60-689476帕。通常，第一部分200包含原料空气100的10％-30％。所生成的经透平膨胀的第一部分204经热交换器202间接热交换而被冷却，所生成的经冷却、透平膨胀后的第一部分作为气流206送入第一塔105中。经压缩的原料空气的第二部分103完全流过热交换101而被冷却，然后流入第二透平膨胀机102中进行膨胀至压力范围一般为413685.60-689476帕。所生成的经透平膨胀的空气104被送入第一塔105中，第一塔的运行压力通常为413685.60-689476帕。第二部分103常含原料空气100的40％-60％。在图1所示的最佳实施例中，经透平膨胀的第一和第二部分汇合在一起作为单股气流206流入塔105中。透平膨胀机201的膨胀温度高于透平膨胀机102的膨胀温度。通常，这两台膨胀机之间的温度差为50K-70K。这样在高温级和低温级上都能供冷，以便在无需给主原料气流输入额外能量的条件下，其液体产量增加而超过单级透平膨胀***。
将经压缩的原料空气的第三部分106送入冷凝器107中，在该冷凝器中，通过与从空分设备中抽出的正蒸发的液体进行间接热交换，使其至少部分被冷凝。通常，第三部分106包含原料空气100的5％-30％。所生成的液体被送入塔105中，液体入塔的进料口位置高于蒸汽的进料口位置。在气流106仅部分冷凝的情况下，所生成的流体160可以直接流入塔105中，或者也可以如图1所示，被送入分离器108中。液体109 从分离器108中流出，再进入塔105中。在进入塔105之前，液体109也可以流经热交换器110而被进一步冷却。冷却冷凝过的部分原料空气可以提高生产过程中的液体产量。
从分离器108中流出的蒸汽111可以直接送入塔105中，或者也可以在热交换器112中与回流进行热交换而被冷却或冷凝，然后再流入塔105中。此外，原料空气的第五部分可以通过在热交换器112中与回流进行热交换而被冷却或被冷凝，然后进入塔105中。可以利用气流111和113来调节原料气中待进行透平膨胀部分的温度。例如，增大气流113的流量，可以提高热交换器112中回流的温度，从而使原料气流的温度增加。两台透平膨胀机的入口温度增加，则能增加产冷量，并能控制被膨胀空气的排出温度，以避免含有任何液体。如果该空分设备包括一个氩塔，原料空气的第四部分120可以通过间接热交换，例如在热交换器122中与氩塔中所产生的流体进行间接热交换而被进一步冷却或冷凝，然后再流入塔105中。
引入第一塔105中的流体在该塔内通过低温精馏被分成富氮和富氧流体。在图1所示的实施例中，第一塔是双级塔***的高压塔。从塔105中抽出富氮蒸汽161，并使其在紧靠沸腾塔130底部的再沸器162中冷凝，生成的液体163被分成液流164和液流118，流体164作为液体回流返回到塔105中，流体118在热交换器112中过冷却，然后快速流入空分设备的第二塔130中。第二塔130的运行压力低于第一塔105的运行压力，通常其运行压力范围为103421.40-206842.80帕。可以从快速流入塔130之前的液流118中回收液氮产品，或者如图1所示，可以直接从流出塔130的液流119中提取液氮产品，以使容器的快速流入间断(flashoff)减至最小。
从塔105中抽出的富氧液体为液流117，该液流在热交换器112中过冷却，然后进入塔130中。如图1的实施例所示，如果空分设备包括一个氩塔，全部或部分液流117可以快速流入冷凝器131中，该冷凝器用于冷凝氩塔顶部的蒸汽。所生成的流体165和166分别为蒸汽和液体，它们从冷凝器131流入塔130中。
在塔130内，通过低温精馏将流体分离成富氮蒸汽和富氧液体。从塔130中抽出的富氮蒸汽为蒸汽流114，该蒸汽流流过热交换器112和101时被复热到近似于环境温度，并作为产品氮气被回收。为了控制塔的洁净程度，从塔130上富氮和富氧进料口之间的某处抽出富氮废气流115，并在将其释放到大气之前，使其流过热交换器112和101，而被复热。采用本发明，氮气的回收率可高达90％或更高。
正如上面所提到的，图1所示的实施例包括空分设备中的一个氩塔。在该实施例中，主要含有氧气和氩气的气流134从塔130流入氩塔132，在氩塔中，通过低温精馏将该气流分离成富氧液体和富氩蒸汽。富氧液体作为液流133返回到塔130中，富氩蒸汽167被送到氩塔冷凝器131中，与富氧流体进行热交换而被冷凝，以便生产富氩液体168。富氩液体的一部分169用作塔132的回流液体，富氩液体的另一部分121作为粗氩产品被回收，通常该产品含氩的浓度超过96％。如图1所示，粗氩产品流121在进一步浓缩和回收之前，可以在热交换器122中与原料气流120进行热交换而被复热或蒸发。
将富氧液体140从塔130中抽出，最好借助高度的变化，即形成液压头、用泵、用加压的贮罐、或者可以将上述方法任意组合使其增压至高于塔130中的压力。在图1所示的实施例中，富氧液体140通过泵141被加压而产生高压液流142。然后该高压液体通过热交换器110而被复热，并节流进入侧冷凝器或产品煮沸器107中，在上述热交换器中，至少部分液体被蒸发。气态产品氧143从冷凝器107中流出，经过热交换器101而被复热，并作为氧气产品被回收。此处所使用的术语“回收”指的是对气体或液体进行处理的任何措施，包括排入大气。液体116可以从冷凝器107中抽出，经热交换器112而被过冷却，再作为液氧产品被回收。
从塔105底部流出的液体的含氧量低于不使用空气冷凝器的传统工艺中液体的含氧量。与传统工艺相比，这就改变了塔105底部及塔130所有段的回流率。本发明由于制冷时无须从塔105中抽取蒸汽或向塔130补充蒸汽，所以产品回收率高。
采用从透平机向塔130补充空气蒸汽或将从塔105中排出的氮蒸汽送入透平机中的方法来获得冷量都会减少塔130中的回流率，并大大降低产品的回收率。本发明则能很方便地保持高回流率，因而产品回收率高，产品纯度也高。采用本发明的***，氧气回收率可高达99.9％，回收的氧气产品的纯度通常可保持在95％-99.95％的范围。
在原料空气进入热交换器101之前先将其分流则可以获得更大的灵活性。如果液体生产的需求与产品压力需求不匹配，则可以供给两种不同压力的空气。提高产品压力将提高产品煮沸器所需的空气压力，而增加液体需求量则会提高透平机入口的空气压力。
图1实施例示出了生产氧气产品所需的原料空气的冷凝作用。图2表示ΔT为1K和2K时在产品沸腾的压力范围内生产氧气产品所需的空气冷凝压力。在任何间接热交换器中，流体之间都存在一定的温差(ΔT)。增加热交换器表面积和/或传热效率可减小流体之间的温差(ΔT)。对于确定的氧气压力要求，减小ΔT可使空气压力降低，同时可减少压缩空气所需的能量，并降低运行费用。
很多参数都影响生产纯净液体，由于透平机流量、压力、入口温度和效率决定产冷量，所以它们都有显著的影响。空气入口压力、温度和热端ΔT将决定热端损失。总液体产量(表示为空气的一部分)取决于透平机的进、出口空气压力、透平机入口温度、透平机效率、主热交换器入口温度以及所生产的高压产品气的产量。生产作为高压产品的气体需要向空气压缩机输入电能以取代产品压缩机所需的电能。
当前，在低温精馏中逐渐用填料来取代塔盘作为汽-液接触部件。结构定形填料或无规填料具有能使塔增加几段而不会显著提高塔的运行压力的优点。这有利于最大限度地提高产品的回收率、增加液体产量和提高产品纯度。由于结构定形填料的性能更易预测，所以结构定形填料优于无规填料。本发明非常适合采用结构定形填料。尤其是在第二塔或低压塔中采用结构定形填料作部分或全部汽-液接触部件是极为有利的。如果采用氩塔，在氩塔内使用这种填料也很有利。
本发明可获得高的产品输送压力，这将减少或抵消产品压缩费用。此外，如果需要某些液体产品，也可以用本发明来生产，所需投资较少。
本发明的***能大大增加设备的制冷量而不必输入附加能量。这就能增加空分设备的液体产量，并使设备在需求量低于设计值和高于设计值的条件下运行效率都较高。所增加的冷量一部分由较高温的透平膨胀所产生，高温透平膨胀之后接着进行冷却，以便进行低温透平膨胀，高温透平膨胀及随后的冷却步骤可以从处于高温水平的加热流体中回收更多的冷量。这样，热交换器202的冷端温差就较小，从而提高了循环的总效率，因为双级、两种温度的透平膨胀比单级低温透平膨胀制冷效率更高。
虽然，我们结合一个具体的实施例详细地描述了本发明，但本领域的普通专业技术人员应意识到，在本权利要求书所描述的实质内容的范围内，还可以有其它一些实施例。

Claims (22)

1.利用低温精馏分离空气以生产气体产品方法，其中包括：
(D)将流入第一塔的流体分离成富氮和富氧流体，并将此两股
   流体引入空分设备的第二塔，第二塔的运行压力低于第一
   塔的运行压力；
(E)将上述流入第二塔的流体分离成富氮蒸汽和富氧液体；和
(G)回收经步骤(F)中热交换而生成的蒸汽，以当作氧气产
   品，
其特征在于：
(A)透平膨胀经冷却、压缩的原料空气的第一部分，对透平膨胀
   过的第一部分进行冷却，将所生成的冷却、透平膨胀过的
   第一部分送入空分设备的第一塔，第一塔的运行压力范围
   一般为413685.60-689476帕；
(B)冷却压缩过的原料空气的第二部分，将已冷却的第二部分
   在低于步骤(A)中透平膨胀温度的温度下进行透平膨胀，
   将所生成的经透平膨胀的第二部分引入第一塔；
(C)至少部分冷凝原料空气的第三部分，将所生成的液体引入
   第一塔；以及
(F)通过与原料空气的第三部分间接热交换来蒸发富氧液体，
   以进行步骤(C)中的冷凝。
2.如权利要求1所述的方法，其特征是经步骤(C)中冷凝而生成的液体在其被送入第一塔之前被进一步冷却。
3.如权利要求1所述的方法，其特征是富氧液体在进行步骤(F)中的蒸发之前被复热。
4.如权利要求1所述的方法，其特征是富氧液体在进行步骤(F)中的蒸发之前被加压。
5.如权利要求1所述的方法，其特征是空分设备还包括一个氩塔，流体从第二塔进到氩塔，并被分离成富氩蒸汽和富氧液体，冷凝富氩蒸汽并至少回收一部分。
6.如权利要求5所述的方法，其特征是通过与富氧流体间接热交换而冷凝富氩蒸汽，以生产富氩液体。
7.如权利要求6所述的方法，其特征是通过与经冷却、压缩的原料空气的第四部分进行间接热交换而使富氩液体蒸发，将所得到的经冷凝的第四部分送入第一塔。
8.如权利要求1所述的方法，其特征是部分冷凝原料空气的第三部分，将所生成的蒸汽再冷凝，然后送入第一塔。
9.如权利要求1所述的方法，其特征是还包括从空分设备中抽出液体，将上述液体作为产品液体而进行回收。
10.如权利要求9所述的方法，其特征是上述产品液体是富氧液体。
11.如权利要求9所述的方法，其特征是上述产品液体是富氧液体。
12.如权利要求1所述的方法，其特征是将从步骤(C)中所生成的液体送入第一塔，其进料口位置高于步骤(A)中所生成的蒸汽进料口位置，或高于步骤(B)中所生成的蒸汽进料口位置。
13.如权利要求1所述的方法，其特征是还包括通过与从空分设备中取出的流体进行间接热交换来冷却原料空气的第五部分，此部分空气的压力或高于透平膨胀过的第一部分的压力，或高于透平膨胀过的第二部分的压力，将所生成的第五部分送入第一塔。
14.如权利要求1所述的方法，其特征是还包括回收作为产品氮气的富氮蒸汽。
15.用于实施权利要求1所述方法的低温空气分离设备，其中包括：
(A)一个空气分离设备，包括：
   一个第一塔、一个第二塔、一个再沸器、将流体从第一塔
   引到再沸器的装置、及将流体从再沸器引到第二塔的装置；
   和
(F)从该冷凝器回收产品气体的装置，
(B)一个第一透平膨胀机，向第一透平膨胀机供给原料空气的
   装置、将流体从第一透平膨胀机送到热交换器的装置、及
   将流体从热交换器送到第一塔的装置；
(C)一个第二透平膨胀机、冷却原料空气并将冷却过的原料空
   气送至第二透平膨胀机的装置，以及将流体从第二透平膨
   胀机送至第一塔的装置；
(D)一个冷凝器、向该冷凝器供给原料空气的装置、及将流体
   从冷凝器送至第一塔的装置；以及
(E)将流体从空分设备送至冷凝器的装置。
16.如权利要求15所述的设备，其特征是还包括提高从空分设备流到冷凝器的流体的压力的装置。
17.如权利要求15所述的设备，其特征是还包括提高从空分设备流到冷凝器的流体的温度的装置。
18.如权利要求15所述的设备，其特征是该空分设备还包括一个氩塔以及将流体从第二塔送至氩塔的装置。
19.如权利要求18所述的设备，其特征是还包括一个氩塔冷凝器、将蒸汽从氩塔送至氩塔冷凝器的装置、将液体从氩塔冷凝器送至氩塔热交换器的装置、将原料空气送至氩塔热交换器以及从氩塔热交换器送至第一塔的装置。
20.如权利要求15所述的设备，其特征是第一塔内装有由结构定形填料构成的汽-液接触部件。
21.如权利要求15所述的设备，其特征是第二塔内装有由结构定形填料构成的汽-液接触部件。
22.如权利要求18所述的设备，其特征是氩塔内装有由结构定形填料构成的汽-液接触部件。
CN91105298A 1990-06-27 1991-06-26 低温空气分离方法和设备 Expired - Fee Related CN1057380C (zh)

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EP0464636B1 (en) 1993-09-22
KR960003273B1 (ko) 1996-03-07
EP0464636B2 (en) 1998-06-24
ES2044653T5 (es) 1998-08-16
CN1058467A (zh) 1992-02-05
CA2045740C (en) 1994-05-17
KR920000365A (ko) 1992-01-29
JPH04227457A (ja) 1992-08-17
DE69100399T3 (de) 1998-11-19
DE69100399T2 (de) 1994-01-13
BR9102696A (pt) 1992-02-04
DE69100399D1 (de) 1993-10-28
US5108476A (en) 1992-04-28
ES2044653T3 (es) 1994-01-01
CA2045740A1 (en) 1991-12-28
EP0464636A1 (en) 1992-01-08

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