CN1165735C - 制备气体产品的低温精馏方法和设备 - Google Patents

制备气体产品的低温精馏方法和设备 Download PDF

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CN1165735C
CN1165735C CNB991062981A CN99106298A CN1165735C CN 1165735 C CN1165735 C CN 1165735C CN B991062981 A CNB991062981 A CN B991062981A CN 99106298 A CN99106298 A CN 99106298A CN 1165735 C CN1165735 C CN 1165735C
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K·K·王
M·J·洛克特
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D·P·波纳奎斯特
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V·斯里尼瓦桑
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J·K·霍维尔
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Abstract

一种制备气体产品的低温精馏方法以及通过该低温精馏制备气体产品的设备，所述低温精馏方法包括：(A)将进料空气于环境温度下在主换热器中冷却并将冷却的进料空气通入低温空气分离装置中；(B)通过低温精馏将低温空气分离装置中的进料空气分离以产生蒸气和液体；(C)将低温空气分离装置中的液体通入分相器且将分相器中的液体通入主换热器；(D)在主换热器中，通过与正在冷却的进料空气的间接热交换使主换热器中来自分相器的液体部分蒸发出分相器，并使蒸发后所得到的流体返回到分相器中；(E)从分相器中获取作为气体产品的蒸气，该方法的特征在于：在步骤(C)中所述低温空气分离装置中的液体直接或经用以增加所述液体压力的液体泵通入所述分相器。

Description

制备气体产品的低温精馏方法和设备
技术领域
本发明涉及进料空气的低温精馏，尤其是制备高压气体产品的进料空气的低温精馏。
背景技术
通常，在制备一种或多种产品比如氧的进料空气低温精馏中，希望能够回收高压气体。达到此要求的一种方法是在高压下操作低温空气分离设备的塔或一组塔，且直接从蒸馏塔回收到高压气体产品。但是，因为塔内的高压加重了分离的负荷，这样的装置总体来说存在缺陷。优选在相对较低的压力下在塔内进行最后的分离，并且，如果要得到高压气体产品，则将产品从塔中抽出，并在回收前增压。
为了获取高压气体产品，可以将产品以气体形式从塔中抽出后压缩至所需压力，然而，更优选以液体形式从塔中抽出后，用泵增压至所需压力，然后在产品蒸发器中蒸发以得到所需的高压气体。
典型的产品蒸发器是与装置中其他的换热器分离的池式热交换蒸发器，这样的排列非常有效但费用高。一般希望产品蒸发器与装置中的主换热器合在一起，并且其排列也是已知的。然而，有时将产品蒸发器与主换热器合在一起会导致沸腾至干涸的问题，其中残留的碳氢化合物在氧中的浓度升高而产生易燃的问题和潜在的危险。
发明内容
因此，本发明的目的之一是提供一种制备高压气体产品的低温精馏装置，这种装置将产品蒸发器与主换热器合在一起，并且能够避免因沸腾至干涸而产生的任何危险。
本领域技术人员在阅读本公开文件后将会很明确本发明所要达到的上述及其它目的，其一方面是：
一种制备气体产品的低温精馏方法，包括：
(A)将进料空气于环境温度下在主换热器中冷却并将冷却的进料空气通入低温空气分离装置中；
(B)通过低温精馏将低温空气分离装置中的进料空气分离以产生蒸气和液体；
(C)将低温空气分离装置中的液体通入分相器且将分相器中的液体通入主换热器中；
(D)在主换热器中，通过与正在冷却的进料空气的间接热交换使主换热器中来自分相器的液体部分蒸发出分相器，并使蒸发后所得到的流体返回到分相器中；
(E)从分相器中获取作为气体产品的蒸气。
该方法的特征在于：在步骤(C)中所述低温空气分离装置中的液体直接或经液体泵通入分相器。
本发明的另一方面是：
一种通过低温精馏制备气体产品的设备，包括：
(A)主换热器及使进料空气于环境温度下进入主换热器的辅件；
(B)低温空气分离装置，包括至少一个塔及使主换热器中的进料空气进入低温空气分离装置的辅件；
(C)分相器及使低温空气分离装置中的液体进入分相器的辅件；
(D)使分相器中的液体进入主换热器的辅件，自分相器进入主换热器的液体通过与主换热器中正的被冷却的进料空气的间接热交换而部分蒸发，使蒸发后所得到的流体进入分相器的辅件；
(E)从分相器获取气体产品的辅件，
其特征在于：(C)辅件将所述低温空气分离装置中的液体直接或经液体泵通入分相器。
本文件中使用的术语“产品蒸发器”是指一种换热器，其中来自低温空气分离装置的通常处于高压的液体通过与进料空气进行间接热交换而蒸发。本发明在实施时，产品蒸发器包括主换热器的一部分。
本文件中使用的术语“进料空气”是指主要含有氧和氮的混合物，比如环境空气。
本文件中使用的术语“塔”是指蒸馏或分馏塔或段，即接触塔或段，在其内部，液相和气相逆流接触进行流体混合物的分离，例如，接触的方式为气相和液相在塔内安装的一系列垂直排列的塔盘或塔板上和/或在有序或随机填充的填料单元上进行接触。关于蒸馏塔的进一步讨论，参见《化学工程师手册》(第五版，R.H.Perry和C.H.Chilton编，纽约Mc Graw-Hill出版公司)第13节“连续蒸馏方法”。
术语“双塔”是指一种高压塔，其上端可与低压塔的下端进行热交换。关于双塔的进一步讨论参见Ruheman的《气体分离》(牛津大学出版社，1949年)第三章工业空气分离。
蒸气和液体接触分离过程取决于各组分间蒸气压的差异。高蒸气压(或易挥发或低沸点)组份将在气相中浓缩，而低蒸气压(或不易挥发或高沸点)组分将在液相中浓缩。部分冷凝是指一种分离方法，通过该方法冷却蒸气混合物，用以在气相中浓缩挥发组分和在液相中浓缩不易挥发的组份。精馏或连续蒸馏是指通过逆流处理气相和液相将连续部分气化和冷凝结合起来的分离方法。一般来说，气相和液相的逆流接触是绝热的，可包含相之间的积分(分段)或微分(连续)接触。利用精馏原理分离混合物的分离过程的排布常可以互换地称为精馏塔、蒸馏塔或分馏塔。低温精馏是指至少部分在150K或更低温度下进行的精馏过程。
本文件中使用的术语“上部”或“下部”是分别指高于和低于分离塔中点的塔段。
本文件中使用的术语“间接热交换”是指这样的热交换，即两种流体相互间不进行任何物理接触或相互混合的热交换过程。
本文件中使用的术语“主换热器”是指与低温空气分离过程结合的主换热器，在其中，进料空气经过与蒸馏中的回流液进行间接热交换而被从室温冷却至蒸馏所需的低温。主换热器中也能包含再冷却塔液流和/或蒸发产品液流。
本文件中的术语“分相器”是指一种具有足够的截面积的容器，可以使进入其中的两相流体依靠重力分离成随后可以分别从分相器中移走的气体和液体组分。
附图说明
图1是本发明的一个优选实施例的示意图，其中，低温空气分离装置含有一个双塔，并且分相器与主换热器分开放置。
图2是可用于本发明中的积分产品蒸发器的一个优选实施例的截面图，其中，分相器与主换热器放置在一起。
具体实施方式
下面结合附图对本发明进行详细的描述。参见附图1，进料空气1通过底部空气压缩机2被压缩，经压缩的空气3经过冷却器4移走压缩热而被冷却。冷却后的压缩空气5经过预净化器6除去高沸点的杂质如水蒸气、二氧化碳和碳氢化合物而得到预净化的进料空气7。
在附图1中所示的本发明的实施例中，预净化进料空气7被分成三部分。其中一部分8经过主换热器9而被冷却，冷却后的进料气流10通入还含有二级或低压塔12的低温空气分离装置中的一级或高压塔11。预净化的进料空气7的另一部分13通过压缩机14被压缩至较高压力，然后通过主换热器9被冷却。冷却后的进料气流15通过涡轮膨胀机16进行膨胀，产生制冷作用，经膨胀的进料气流17通入低压塔12。预净化进料空气7的另一部分18经过压缩机19被压缩至较高压力，然后经过主换热器9进行冷却或更优选的是至少进行部分冷凝。然后将得到的进料气流20通入高压塔11。
高压塔11通常在绝对压力为65-90磅/平方英寸(psia)的压力范围进行操作。进料空气在高压塔11内经低温精馏分离成富氮蒸气和富氧液体。富氧液流21从高压塔11的下部抽出，通过主换热器9被再冷却成液流22后进入低压塔12。富氮蒸气流23从高压塔11的上部抽出，通入主冷凝器24，在那里，通过与低压塔12底部液体进行间接热交换而被冷凝。冷凝后的富氮液体25被分成返回高压塔11进行回流的部分26和通过主换热器9进行再冷却后作为液流28进入低压塔12的上部进行回流的部分27。
低压塔12在低于高压塔11的压力下操作，压力范围通常为19-30psia。进入低压塔12中的各种物料经低温精馏被分离成富氮蒸气和富氧液体。从低压塔12的上部抽出富氮蒸气流29，经主换热器9进行加热，并且由装置中出来的氮气流30可以全部或部分作为氮气产品回收，其中的氮的浓度至少为99％(mol)。为了控制产品的纯度，废气流31从低压塔12的上部低于气流29的抽出位置抽出，经过主换热器9的加热，并作为气流32从装置中抽出。
氧浓度至少为85％(mol)一般在95-99.8％(mol)的范围内的富氧液体33，从低压塔12的下部抽出。优选如附图1中所示，富氧液体经液体泵34泵至较高压力而产生被加压的富氧液体流35。当供给产品蒸发器的液体的压力在15-55psia范围内时，本发明更具效用。如果需要的话，富氧液体35经泵后的部分36可以作为液体氧产品回收。
富氧液体35经过分相器37，经过分相器后的液流38进入主换热器9的产品蒸发器段经与正被冷却的进料空气进行间接热交换而被部分气化。控制富氧液流38的流速以确保产品蒸发器段的液体得以部分气化。产品蒸发器中得到的两相流体39返回至分相器37，蒸气40从分相器37中抽出并以气态产品的形式得到所含氧的浓度至少为85％(mol)的气体氧产品。如附图1所示，优选气态氧流40经主换热器9加热后得到气流41。因为使用了分相器，避免了换热器内的液体完全蒸发，从而避免了沸腾至干涸的情况，在干涸的情况下会使富氧液体中的碳氢化合物浓缩并产生险情。
在附图1中所描述的本发明的实施方案中，分相器与主换热器中的产品蒸发器段分开放置。优选将分相器与产品蒸发器段放置在一起，一个这样的实施方案如附图2所示。
如附图2所示，产品蒸发器段50与分相器51放置在一起，中间有垂直的间隔条52。附图2所示的实施方案构成主换热器的下部，且图中所示为横截面。正如在换热器技术中所公知的，通过交替放置板和翅片，利用连接的分隔棒和分配器导入和收集各通道的流体，从而形成沸腾通道61和冷却通道60。低温空气分离装置中的液体53经入口54进入分相器51中，在分相器51中形成液池55。如果需要的话，可以从分相器51中获取液体产品流56。
液池55中的液体通入产品蒸发器50的热交换通道61的底部，借助液池55的液头压力，往上至热交换通道。在热交换通道内，向上流的液体通过与通道60中向下流的正被冷却的进料空气的间接热交换而被部分气化。得到的两相流体便流出热交换通道的顶部并返回到分相器51。两相流体中的液体57落入液池55中并成为其中的一部分，同时两相流体中的蒸气58通过出口59流出分相器51而获取气体产品。附图2中所示的实施例中，在获取前，将气体产品经主换热器加热。尽管产品蒸发器段50通常位于主换热器9的底部，但应明确进料空气冷却通道60能够扩展至主换热器的整个长度。进料空气冷却流20首先在主换热器的上部借助返回流被冷却，然后在主换热器的下部即产品蒸发器段被进一步冷却和冷凝。
尽管本发明根据一定的优选的实施例进行了详细的描述，但本领域技术人员将会认识到，在本发明的权利要求的构思和范围内，本发明还有其它的实施方案。例如，可以使用其它低温空气分离装置，如带有氩(argon)侧臂塔和/或向上流侧塔的双塔的装置。

Claims (8)

1.一种制备气体产品的低温精馏方法，包括：
(A)将进料空气于环境温度下在主换热器中冷却并将冷却的进料空气通入低温空气分离装置中；
(B)通过低温精馏将低温空气分离装置中的进料空气分离以产生蒸气和液体；
(C)将低温空气分离装置中的液体通入分相器且将分相器中的液体通入主换热器；
(D)在主换热器中，通过与正在冷却的进料空气的间接热交换使主换热器中来自分相器的液体部分蒸发出分相器，并使蒸发后所得到的流体返回到分相器中；
(E)从分相器中获取作为气体产品的蒸气，
该方法的特征在于：在步骤(C)中所述低温空气分离装置中的液体直接或经用以增加所述液体压力的液体泵通入所述分相器。
2.如权利要求1所述的方法，其中低温空气分离装置中的液体为所含氧的浓度至少为85％mol的富氧液体。
3.如权利要求1所述的方法，其中分相器中的蒸气在获取前通过与正在冷却的进料空气进行间接热交换而被加热。
4.通过低温精馏制备气体产品的设备，包括：
(A)主换热器及使进料空气于环境温度下进入主换热器的辅件；
(B)低温空气分离装置，包括至少一个塔及使主换热器中的进料空气进入低温空气分离装置的辅件；
(C)分相器及使低温空气分离装置中的液体进入分相器的辅件；
(D)使分相器中的液体进入主换热器的辅件，自分相器进入主换热器的液体通过与主换热器中正在被冷却的进料空气的间接热交换而部分蒸发，使蒸发后所得到的流体进入分相器的辅件；
(E)从分相器获取气体产品的辅件，
其特征在于：(C)辅件将所述低温空气分离装置中的液体直接或经液体泵通入分相器。
5.如权利要求4所述的设备，其中分相器与主换热器分开放置。
6.如权利要求4所述的设备，其中分相器与主换热器一起放置。
7.如权利要求4所述的设备，其中低温空气分离装置包括带高压塔和低压塔的双塔及使低温空气分离装置中的液体进入与低压塔下部连通的分相器的辅件。
8.如权利要求4所述的设备，其中从分相器中获取气体产品的辅件包含使分相器中的蒸气通过主换热器的辅件。
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