CN1058466A - 生产高压气体产品的低温空气分离系统 - Google Patents

生产高压气体产品的低温空气分离系统 Download PDF

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CN1058466A
CN1058466A CN91105297A CN91105297A CN1058466A CN 1058466 A CN1058466 A CN 1058466A CN 91105297 A CN91105297 A CN 91105297A CN 91105297 A CN91105297 A CN 91105297A CN 1058466 A CN1058466 A CN 1058466A
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J·R·德雷
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Union Carbide Industrial Gases Technology Corp
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Abstract

本发明公开了一种低温空气分离系统，在该系统 中一部分原料空气被透平膨胀以产生冷量，原料空气 的第二部分与从空分设备中流出的正在蒸发的产品 进行热交换而被冷凝，此两部分原料空气均被送入同 一塔中以进行分离。

Description

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产品气体。
常用于空气分离的工业系统是低温精馏，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系统之前经压缩机压缩而获得的。进行空气分离时，液体和蒸汽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，低温分离是在主塔系统和辅助氩塔中进行的，主塔系统至少包括一个塔，在该塔中原料空气被分离成富氮组分和富氧组分，从主塔系统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系统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，这种系统很有效，但十分昂贵。
因此，本发明的一个目的是要提供一种改进的低温空气分离系统。
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系统。
本发明还有一个目的是要提供一种具有较高的氩气回收率的低温空气分离系统。
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。本发明一般包括透平膨胀一部分经压缩的原料气，以向设备供冷并提高氩气的回收率;冷凝另一部分与正蒸发的液体进行热交换的原料空气，以生产产品气体。
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产品气体的方法，它包括如下步骤：
（A）透平膨胀经冷却、压缩的原料空气的第一部分，将所生成的经透平膨胀的部分引入空分设备的第一塔中，第一塔的运行压力范围通常为60至100磅/吋2;
（B）至少部分冷凝经冷却、压缩的原料空气的第二部分，将所生成的液体引入上述第一塔;
（C）将进入上述第一塔的流体分离成富氮流体和富氧流体;并将上述两股流体引入空分设备的第二塔中，所述第二塔的运行压力低于上述第一塔的运行压力;
（D）将流入第二塔中的流体分离成富氮蒸汽和富氧液体;
（E）通过与经冷却、压缩的原料空气的第二部分进行间接热交换蒸发富氧液体，以便进行步骤（B）中的冷凝;
（F）回收经步骤（E）中热交换而获得的蒸汽，以作为氧气产品;以及
（G）将从第二塔流出的含氩流体送入氩塔;将含氩流体分离成富氧液体和富氩蒸汽，回收至少部分富氩流体。
本发明另一方面包括：
利用低温精馏分离空气以生产产品气体的设备，它包括：
（A）一个空气分离设备，它包括：
一个第一塔、一个第二塔、一个再沸器、使流体从第一塔流入再沸器的装置、以及使流体从再沸器流到第二塔的装置;
（B）一个透平膨胀机、向透平膨胀机提供原料空气的装置、以及使流体从透平膨胀机流到第一塔的装置;
（C）一个冷凝器、向该冷凝器提供原料空气的装置、以及使流体从该冷凝器流进第一塔的装置;
（D）使流体从空气分离设备流入上述冷凝器的装置;
（E）从上述冷凝器回收产品气体的装置;以及
（F）一个氩塔、使流体从第二塔流入该氩塔的装置、以及从上述氩塔中回收流体的装置。
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  of  Gases）”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系统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90至500磅/吋2（psia）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。将经冷却、压缩的原料空气的第一部分103送入透平膨胀机102中，膨胀后的压力通常为60到100磅/吋2。将所生成的膨胀后的空气104送入第一塔105中，该塔的运行压力范围一般为60-100磅/吋2。通常第一部分103含有70%-90%的原料气100。
将冷却、压缩后的原料气的第二部分106送入冷凝器107中，在该冷凝器中，此部分原料气与来自在后面将作更详细描述的空分设备的正在蒸发中的富氧液体进行间接热交换而至少部分被冷凝。通常，第二部分106含有原料空气100的5%-30%。所生成的液体从高于蒸汽进料口的地方被送入塔105中。在气流106仅部分被冷凝的情况下，所生成的流体160可以直接送入塔105中，或者如图1所示，送入分离器108中。从分离器108流出的液体109再流入塔105中。液体109也可以在进入塔105之前流过热交换器110而进一步被冷却。对原料空气中经过冷凝的部分进行冷却可以提高生产过程中液体的产量。
从分离器108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，被冷却、压缩的原料气的第四部分113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。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103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，从而也提高了气流103的温度。透平膨胀机102的入口温度增高，可以提高产冷量，而且还能控制膨胀气体的出口温度，以避免含有任何液体。经冷却、压缩的原料气的第三部分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。
在第一塔105中，通过低温精馏，原料气被分离成富氮流体和富氧流体。在图1所示的实施例中，第一塔是双级塔系统的高压塔。将富氮蒸汽161从塔105中抽出，然后在紧靠沸腾塔130底部的再沸器162内冷凝。生成的液体163被分成液流164和液流118，液流164作为液体回流返回到塔105中，液流118在热交换器112内过冷，然后快速流入空分设备的第二塔130内。第二塔130以低于第一塔的压力运行，通常压力在15-30磅/吋2的范围内。可以从快速流入塔130之前的液流118中回收液氮产品，或如图1所示，可以直接从塔130中流出的液流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，然后流入塔130中。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。所得到的流体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中，流入该塔内的流体通过低温精馏被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。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。废气流115的一部分可用于再生吸附床，以便清洁原料空气。采用本发明，氮气的回收率可高达90%或更高。
主要含有氧气和氩气的气流134从塔130流入氩塔132，在该氩塔中，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从而被冷凝，以生产富氩液体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内与原料空气流120进行热交换而被复热或蒸发。
本发明由于将一部分原料气在进入高压塔之前进行膨胀而产生冷量，因此特别有利于获得氩气的高回收率。这样能使低压塔的液体输入量达到最大，并且提高了塔内的回流率。而将从高压塔流出的蒸汽或进入低压塔的空气进行膨胀的其它系统流入低压塔的液体量却很少。
将富氧液体140从塔130中抽出，并将其增压至高于塔130中的压力，增压的方法可以借助高度的变化，即如图1所示那样形成液压头、用泵、用加压的贮罐、或者也可以将上述方法任意组合。然后该液流通过热交换器110而被加热，并流入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，通过热交换器101时被复热，并作为产品氧气被回收。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，包括将它们排入大气。液体116可以从冷凝107中抽出，通过热交换器112而过冷，再作为液氧产品被回收。通常氧气产品的纯度为99.0%-99.95%。采用本发明，氧气回收率可高达99.9%。
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底部和塔130所有段的回收率。本发明由于制冷时无须从塔105中抽取蒸汽或向塔130中补充蒸汽，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中排出的氮蒸汽送到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，因而可保持高的产品回收率。
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2表示△T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（△T）。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（△T）。对于确定的氧气压力要求，减小△T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△T将决定热端的损失。总产液量（表示为空气的一部分）取决于透平机进出口空气压力、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。本发明非常适宜采用结构定形填料。尤其在第二塔或低压塔以及氩塔内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。
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，也可以利用本发明来生产，而所需投资较少。与使进入低压塔的空气膨胀的传统系统相比，本发明所需的主热交换器更短而且数量也少。这是因为热传递的驱动力大的缘故。
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 (18)

1、利用低温精馏分离空气以生产气体产品的方法，它包括：
(A)透平膨胀冷却、压缩过的原料空气的第一部分，将透平膨胀所产生的部分引入空分设备的第一塔，通常上述第一塔的运行压力范围为60-100磅/时2；
(B)至少冷凝一些冷却、压缩过的原料空气的第二部分，并将所生成的液体引入第一塔；
(C)将进入第一塔的流体分离成富氮和富氧流体，并将所述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；
(D)将流入第二塔的流体分离成富氮蒸汽和富氧液体；
(E)通过与冷却、压缩过的原料空气的第二部分进行间接热交换使富氧液体蒸发，以便进行步骤(B)中的冷凝；
(F)回收从步骤(E)的热交换中所得到的蒸汽，以作为氧气产品；以及
(G)将从第二塔流出的含氩流体引入氩塔，将上述含氩流体分离成富氧液体和富氩蒸汽，至少回收部分富氩流体。
2、如权利要求1所述的方法，其特征是将冷凝原料空气时所得到的液体在引入第一塔之前进一步冷却。
3、如权利要求1所述的方法，其特征是在富氧液体与正冷凝的原料空气的第二部分进行热交换而被蒸发之前，使其复热。
4、如权利要求1所述的方法，其特征是在富氧液体与处在冷凝过程中的原料空气的第二部分进行热交换而被蒸发之前，使其增加压力。
5、如权利要求1所述的方法，其特征是通过与富氧流体进行间接热交换使富氩蒸汽泠凝，所生成的富氩液体作为富氩流体而被回收。
6、如权利要求5所述的方法，其特征是通过与冷却、压缩过的原料空气的第三部分进行间接热交换来蒸汽富氩液体，将所生成的冷凝后的第三部分送入第一塔。
7、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二部分，将所生成的蒸汽再冷凝，然后送入第一塔。
8、如权利要求1所述的方法，其特征是还包括从空分设备中回收液体产品。
9、如权利要求8所述的方法，其特征是上述液体产品是富氮流体。
10、如权利要求8所述的方法，其特征是上述液体产品是富氧液体。
11、如权利要求1所述的方法，其特征是还包括回收富氮蒸汽以作为氮气产品。
12、利用低温精馏分离空气以生产产品气体的设备，它包括：
（A）一个空分设备，包括：一个第一塔、一个第二塔、一个再沸器、用于使流体从第一塔流到再沸器的装置、以及使流体从再沸器流到第二塔的装置;
（B）一个透平膨胀机、向该透平膨胀机提供原料空气的装置、以及使流体从透平膨胀机流入第一塔的装置;
（C）一个冷凝器，向该冷凝器供给原料空气的装置、及将流体从该冷凝器送入第一塔的装置;
（D）使流体从空分设备流入上述冷凝器的装置;
（E）从冷凝器中回收气体产品的装置;以及
（F）一个氩塔、使流体从第二塔流入上述氩塔的装置、及从氩塔中回收流体的装置。
13、如权利要求12所述的设备，其特征是还包括使从空分设备流到冷凝器的流体增压的装置。
14、如权利要求12所述的设备，其特征是还包括使从空分设备流到冷凝器的流体温度提高的装置。
15、如权利要求12所述的设备，其特征是还包括一个氩塔冷凝器、将蒸汽从氩塔送入氩塔冷凝器的装置、将液体从氩塔冷凝器送到热交换器的装置、向上述热交换器供给原料空气的装置以及将其从热交换器送至第一塔的装置。
16、如权利要求12所述的设备，其特征是在第一塔中装有由结构定形填料构成的汽-液接触部件。
17、如权利要求12所述的设备，其特征是在第二塔中装有由结构定形填料构成的汽-液接触部件。
18、如权利要求12所述的设备，其特征是氩塔中装有由结构定形填料构成的汽-液接触部件。
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CN102537589A (zh) * 2012-01-16 2012-07-04 北京市旭广厦暖通节能设备有限责任公司 用于集中供热的保养提效系统
CN102563285A (zh) * 2012-01-13 2012-07-11 北京市旭广厦暖通节能设备有限责任公司 用于集中供热系统的保养提效方法
CN113154796A (zh) * 2021-03-23 2021-07-23 金川集团股份有限公司 一种回收氧氮资源的可变多循环氧氮冷能利用装置及方法

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CN102563285B (zh) * 2012-01-13 2014-11-19 北京市旭广厦暖通节能设备有限责任公司 用于集中供热系统的保养提效方法
CN102537589A (zh) * 2012-01-16 2012-07-04 北京市旭广厦暖通节能设备有限责任公司 用于集中供热的保养提效系统
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CN113154796A (zh) * 2021-03-23 2021-07-23 金川集团股份有限公司 一种回收氧氮资源的可变多循环氧氮冷能利用装置及方法

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KR920000362A (ko) 1992-01-29
ES2050016T3 (es) 1994-05-01
CN1044156C (zh) 1999-07-14
CA2045737C (en) 1994-05-03
BR9102697A (pt) 1992-02-04
CA2045737A1 (en) 1991-12-28
JP2704916B2 (ja) 1998-01-26
DE69101281T3 (de) 1999-02-25
ES2050016T5 (es) 1998-11-01
DE69101281T2 (de) 1994-06-09
EP0465929A1 (en) 1992-01-15
US5114452A (en) 1992-05-19
EP0465929B1 (en) 1994-03-02
KR960003270B1 (ko) 1996-03-07
JPH04227458A (ja) 1992-08-17
DE69101281D1 (de) 1994-04-07

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