CN1142042A - 液体流蒸发的工艺过程和设备 - Google Patents

液体流蒸发的工艺过程和设备 Download PDF

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CN1142042A
CN1142042A CN96103613A CN96103613A CN1142042A CN 1142042 A CN1142042 A CN 1142042A CN 96103613 A CN96103613 A CN 96103613A CN 96103613 A CN96103613 A CN 96103613A CN 1142042 A CN1142042 A CN 1142042A
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J·P·特兰尼尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及到通过与冷凝气进行热交换而完成液体蒸发的工艺过程，在此过程中，被蒸发液体的压力降低，并且在蒸发完成后液体流中富集挥发性差的组分。根据本发明的另一种可选方式，被冷凝的气体中同样可以富集挥发性差的组分。

Description

液体流蒸发的工艺过程和设备
本发明涉及一种液体蒸发的工艺过程和设备。更具体地说，它是适用于液体蒸发的一种工艺过程，是通过低温蒸馏分离气体混合物的过程的一部分，例如空气蒸馏过程。
通过与一种气体流进行潜热交换(气体流因此而冷凝)来蒸发一种液体流是我们经常所需要做的。本发明涉及到的情况是两种流体至少由两种组份组成。如果所用的液体流比气体流含有较高的挥发性差的组份，那么温度T下的气体流的冷凝压力将会比温度(T－△T)下的液体流的蒸发压力高。
例如，如果不纯净的液氧(95％氧，5％氮)流在5×105Pa的压力下，在与冷凝空气流反向流动过程中被蒸发，那么13×105Pa的空气压力是完全确定的，因为空气具有固定的组成(21％的氧和79％的氮)。这里空气被看作双组份混合物，以便于比较。
同理，如果空气压力保持不变还是13×105Pa，那么纯氮流将在低于14×105Pa数量级的压力下蒸发。
在很多情况下，人们希望降低被冷凝的空气流压力或者升高被蒸发的液体流的压力，但是压力的最小值或最大值是由流体本身的组成所决定的。例如在空气蒸馏过程中，人们希望能尽可能地降低原料空气的压力。
总之，本发明的主体在于通过与要冷凝的气体流进行热交换蒸发液体流的工艺过程，两种流体至少由两种组份组成，并有以下特征：
i)在与气体流进行热交换而实现蒸发之后，液体流富集挥发性差的组份；和/或
ii)在与液体流进行热交换而冷凝之前，气体流富集挥发性差的组份。
根据本发明的其它特点和优点：
-挥发性较差的组份是氧，另一种挥发性较强的组份为氮；
-通过将其输送到一种混合塔的容腔内气体流和/或被蒸发的液体流来富集挥发性差的组份，这种混合塔从顶部注入了一种比被富集的混合物含较多挥发性差的组份的液体。
-气体流在混合塔容腔内的一个交换器中冷凝。
本发明的另一主体涉及到通过与气体流热交换进行液体流蒸发的一种设备，两种流体至少由两种组份组成，含有能使气体流和液体流之间进行热交换的装置，其特征为含有一个可富集挥发差的组份的装置：
i)被蒸发的液体流流向进行热交换的装置的下面；
ii)气体流流向能进行热交换的装置的上面。
根据其它特征：
-这种富集流体(某种组份)的装置包括一个混合塔，混合塔内注入了一种比被富集流体含有较高挥发性差的组份的液体。
-这种能进行热交换的装置包含一个位于混合塔容腔内的交换器，或者一个位于低压塔容腔内的交换器。
下述工艺过程是同样可行的，其中通过与气体流(被冷凝)进行热交换来实现液体流的蒸发，两种流体至少由两种组份组成，液体流比气体液含有较高的挥发性差的组份，并具有以下特点：
i)在与气体流进行热交换而实现蒸发之后，液体流富集挥发性高的组份；
ii)在与液体流进行热交换而实现蒸发之前，气体流富集挥发性高的组份。
这使得在特殊条件下，可以增加被蒸发液体流的压力。
并且人们可以依此设计工艺过程和设备，来改变在此种混合物被蒸发之后和/或被冷凝之前某种混合物中一系列成份的含量。所以，对于一种三元混合物，其中的两种挥发性差的组份可以被富集。
本发明的另一主体涉及通过与气体流热交换进行液体流蒸发的设备，两种流体至少由两种组份组成，液体流比气体流含有较高的挥发性差的组份，设备含有可使气、液体流之间进行热交换的装置，其特征是含有一种可富集挥发性差的组份的装置：
i)被蒸发液体流流向进行热交换的装置下面；
ii)气体流流向进行热交换的装置上面。
根据设备的其它特点：
-富集流体的装置包含一种混合塔，此塔中注入了比被富集流体含有更高挥发性差的组份的液体；
-使热交换成为可能的此种装置包含一个位于混合塔容腔内的交换器，或者一个位于低压塔容腔内的交换器。
本发明的最后一项主体涉及到通过蒸馏来分离气体混合物的整套设备，其中包含上述装置，并且液体流为分离产品，而气体流是被分离的气体混合物。
本发明对低温蒸馏特别有用。
参照附图，下面介绍本发明的两个实施例：
-图1是已知技术中的蒸发设备图；
-图2和图3分别是根据本发明的第一种和第二种选择形式的蒸发设备图；
-图4和图6分别是已知技术中的蒸馏过程装配图；
-图5是根据本发明第二种选择方式对图4进行补充完整的本发明的整体图解；
-图7是根据本发明第一种选择方式对图6进行补充完整的本发明的整体图解。
图1表示一种热交换器60，其中液体流A通过与气体流C进行潜热交换而变为气体流，而气体流C则冷凝为液体流D。A和C两种流体至少由两种组份组成，并且C比A含有较多的挥发性高的组份。例如，A可为不纯净的液氧(95％O2，5％N2)，C可以是空气(79％N2，21％O2)。在这种情况下，如果A在5×105Pa，那么C必须在13×105Pa。
为完成本发明过程，在图2所示的第一步工艺过程中，不纯净的液氧(95％O2，5％N2)流A在5×105Pa压力下在交换器60中继续蒸发。被冷凝的气相空气流C的组成通过将其通入一个混合塔62的容腔内来改变，此混合塔的顶部有组成为70％O2，30％N2的液流F注入。含有40％O2的顶气E从塔62中取出，并且在比空气流C低得多的压力下冷凝。这样就使得气相空气流C的压力降为9×105Pa。
本发明图2同样可用于下述情况，即蒸发是对挥发性高的组份而言，如14×105Pa下的液氮。此时空气流不是在13×105Pa下在图1的交换器60中冷凝，而是将其通入混合塔62，以便在塔顶得到比空气中含有较多氧的富集气。
这样，被冷凝的流体C在冷凝前含有较高的氧含量。
为了完成此发明，图3描述了第二种工艺过程，此时被蒸发的液体组成被改变了。目的是为了获得组成为95％O2的5×105Pa的不纯净氧气流B，组成为21％O2，79％N2的9×105Pa的空气气流C(空气被视为双组份混合物)被冷凝了。
我们选择一种液体A，它含有比我们想要得到的气体流B较少的氧，并且在空气于9巴的冷凝温度下和5×105Pa压力下蒸发。液流A的组成为70％O2，30％N2，在交换器60中蒸发。蒸发完毕后，流体E在混合塔62中富集氧，混合塔62中也注入了组成为98％O2和2％N2的液体流F1。具有所希望组成的气体流B(95％O2和5％N2)将从塔62的塔顶采出。
如此说来，第二种工艺过程所包含的阶段有：被蒸发的液流在蒸发完毕后富集氧，而空气的冷凝压力比同样压力下蒸发不纯净氧时所需要的冷凝压力小。
在传统的泵送液氧设备中，如图4所示，有三股空气流被送进了主交换器，此时主交换器中液氧流在压力下进行蒸发。第一股气流1为13×105Pa，此空气流的剩余物(约70％)被压缩到5×105Pa，并被一分为二。第二股气流2经过交换器7被输送到双蒸馏塔中的中压塔100。第三股气流3被升压机9加压到10×105Pa，在叶轮机11和升压机共同作用下冷却并调节其压到稍高于低压塔102的压力，然后经过一步过冷阶段之后被输送到低压塔102中。
只有第一股气流1由于其较高的压力在交换器7中会液化，它被一分为二，分别注入低压塔和中压塔。
95％不纯净氧产品以液体形式从低压塔102的容腔内采出，并用泵13使其加压到5×105Pa，然后在交换器7中蒸发。
为了减小蒸发氧过程中的空气流压力，本发明图3适用于一种泵输液氧设备，如图5所示，其组成部份与图4相同，并具有相同的数字图标。
大部分压力数值是相同的，只有空气流C的压力只有9×105Pa。空气流C不是在经过交换器7时进行冷凝，而是在混合塔104的冷凝器19中冷凝。含98％氧的不纯液氧从低压塔102的容腔内采出，并经过泵13加压后输送到混合塔104的顶部，而富集液体流从中压塔100的容腔中采出并输送到混合塔104的容腔中。含有所需氧纯度(95％)的气流B从混合塔的顶部采出。在交换器19中蒸发的液相是下面两种液体的混合物，其一为从中压塔100中采出的富集液体相，其二是从混合塔容腔塔板采出的80％O2的液相G’。一种非蒸发的液相G含有76％的O2，并与含55％O2的蒸气E保持平衡，此液相G从容腔内采出并回注到塔中。
图6表示了泵输液氧设备的一种传统图，其目的在于一定压力下从中压塔100和低压塔106两塔中的蒸馏空气来生产氧。102由两个蒸发器/冷凝器组成；中间蒸发器冷凝从中压塔来的顶气(氮气)并回流到两塔的顶部。低压塔106低部的蒸发器21通过蒸发液氧来冷凝空气，从而为此塔的容腔提供热量。此种情况下中压塔的压力决定于蒸发器21中蒸发不纯氧(95％O2)的空气流C的冷凝压力。
液氧从低压塔的容腔中采集，并经过泵13加压到5×105Pa后输送到交换器，并在此通过13×105Pa的空气流的冷凝被蒸发。
为了减小输送到中压塔中的空气压力，本发明的图2可适用于图6的泵输液氧设备。图7表示了这种新设计。
被蒸馏的空气部分，通常用来提供低压塔容腔内的热量，如图2和图6中的气流C，在图7中它却被输送到混合塔108中并与富氧液流F接触，此液流F产生于低压塔的中部并经过泵14加压。通过与液流F的接触，空气流富集氧并产生组成为40％O2，60％N2的流体E，此流体E从塔108中采出并在低压塔中的容腔蒸发器21中冷凝。从混合塔流出的液相G，其氧浓度为40％，并与液相D和从中压塔100中采集的富集液相混合。这些液相被用作低压塔102的回流液。
这种设计安排可使空气压力降低约20％，对主空气压缩机而言将大大地节省能源。
本发明并非仅仅应用于通过与被冷凝的双组份气体流进行热交换而实现双组份液相混合物蒸发的情况，本发明同样适用于单组份液体流的蒸发，此时的气体流应为包含此液相组份的混合气体，还可以包含少量比共同组份更易挥发的另一种气体。
本发明同样可应用于其它气体和其他液体。本发明还可应用于下述情况，即流体B(图2)和E(图3)部分蒸发，而流体D(图2和图3)部分冷凝。

Claims (17)

1.通过与冷凝气流(C)进行热交换而实现液体流(A)蒸发的工艺过程，其中两种流体(A，C)至少由两种组份组成，并具有以下特点：
i)通过与气体流(C)进行热交换而实现蒸发后，液体流(A)富集挥发性差的组份。
ii)通过与液体流(A)进行热交换而实现冷凝前，气流(C)富集挥发性差的组份。
2.根据权利要求1的过程，其中挥发性差的组份是氧，而另一种挥发性较好的组份为氮。
3.根据权利要求1或2的过程，其中气流(C)和/或被蒸发的液流(A)混合物通过把它们输送到有顶液(F)注入的混合塔(104，108)的容腔内而富集挥发性差的组份，并且顶液(F)比被富集的混合物(A，C)含有较多的挥发性差的组份。
4.根据权利要求3的过程，其中气流(C)在位于混合塔容腔中的交换器(19，104)内进行冷凝。
5.根据权利要求3的过程，其中气体流(E)富集挥发性差的组份并在中压/低压双塔系统的低压塔(102，106)中的容腔蒸发器(21)中进行冷凝，所说的低压塔包含一个中间蒸发器，以用来冷凝中压塔(100)的顶气-氮气。
6.根据权利要求3的过程，其中得到不纯净的氧，并且一种富氧液相被蒸发，被蒸发的液相先被输送到混合塔，并在这里与从双塔系统的低压塔容腔内采集的、纯度比上述不纯气态氧稍高的液氧相接触，进行传热和传质，不纯的氧从混合塔的顶部采出。
7.根据权利要求6的过程，其中从混合塔容腔中采出的液体被输送到低压塔。
8.根据权利要求3的过程，其中从低压塔容腔中产生的氧与一种蒸气进行热交换而蒸发，此蒸汽比空气含较多的氧，并从混合塔的顶部采出，在此混合塔中，被蒸馏空气的一部份和从低压塔中部产生的、含较多氧的液体流相接触，进行传质和传热。
9.根据权利要求8的过程，其中在所说的混合塔容腔中产生的液相和所说的被冷凝的蒸汽都被输送到低压塔中。
10.根据权利要求9的过程，其中所说的液相部份是产生于中压塔的富集液相的一部分。
11.根据权利要求10的过程，其中所说的液相部份是富集液相和从混合塔的容腔塔板上采集的液相的混合物。
12.通过与气体流(C)进行热交换而蒸发液体流(A)的设备，两种流体(A，C)至少由两种组份组成，并且此设备含有可使气体流(C)和液体流(A)之间进行热交换的装置(60，19，21)，其特征为含有富集挥发性差组份的装置(62，104，108)：
i)被蒸发的液体流(A)流向能进行热交换的装置(60，19，21)的下部；
ii)气体流(C)流向能进行热交换的装置(60，21)的上部。
13.根据权利要求12的设备，其中富集流体(A，C)的装置(62，104，108)由一个混合塔(104，108)组成，此塔中注入了一种比被富集流体含较多挥发性差的组份的流体(F，F’)。
14.根据权利要求12和13之一的设备，其中能进行热交换的装置包含一个位于混合塔(104)容腔内的交换器，或者一个位于低压塔(102，106)容腔内的交换器。
15.根据权利要求14中的设备，其中低压塔(102，106)的下部(106)位于中间蒸发器的下方，而与位于中压塔上方的上部(102)相分离。
16.用蒸馏法分离气体混合物的整套设备包括根据权利要求13-15之一的一种设备，其中液体流(A)是一种分离产物，而气体流(C)是被分离的气相混合物。
17.根据权利要求16的整套设备，其中液体流(A)是空气的一种或多种组份的加压流体，而气体流(C)是空气。
CN96103613A 1995-03-15 1996-03-15 液体流蒸发的工艺过程和设备 Pending CN1142042A (zh)

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