CN85109265A - 从原料气中分离产品气体的方法及其装置 - Google Patents

从原料气中分离产品气体的方法及其装置 Download PDF

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CN85109265A
CN85109265A CN85109265.9A CN85109265A CN85109265A CN 85109265 A CN85109265 A CN 85109265A CN 85109265 A CN85109265 A CN 85109265A CN 85109265 A CN85109265 A CN 85109265A
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cryogenic
expansion turbine
heat exchanger
normal temperature
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CN1004229B (zh
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守秀治
小山祥二
山崎正博
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Hitachi Ltd
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Abstract

本发明的气体分离方法和气体分离装置用于从原料中分离和提取有价值的气体，如氮气、氧气、氩气等，可以有效地产生低温效应。其流程如下：将低温气体在热交换器中与原料气进行热交换，使其温度回升；该温度回升的气体被送入由膨胀涡轮驱动的升压器加压；加压后的气体被冷却器冷却到常温后进一步在热交换器中冷却；然后该低温气体被送入膨胀涡轮进行绝热膨胀，由此产生低温效应。

Description

本发明叙述了一种分离气体的方法，该方法是通过低温过程从原料气中分离出有价值的气体，如氮气、氧气、氩气等。本发明也叙述了适用于上述气体分离方法的气体分型装置。
众所周知的常规方法是将由气体分离装置分离出的废气引入热交换器，使其与原料空气进行热交换，冷却原料空气，并且同时使该废气在膨胀涡轮中流动，由此产生低温效应。日本专利申请公开79972（1980年）披露了采用上述低温废气的低温过程。该方法提出，将从空气分离装置的氮气冷凝器中放出的低温废气送入热交换器，废气在其中加热恢复至中间温度，然后流入膨胀涡轮进行绝热膨胀，由此产生低温效应的低温废气再进入热交换器，以便使其恢复至常温。采用这种方法，从空气分离装置放出的低温废气全部通过热交换器转移到膨胀涡轮。膨胀涡轮进口处压力由从空气分离装置释放出的低温废气的压力确定，这样进口处压力决不过超过释放出的低温废气的压力。由于上述原因，限制了单位加工气体产生的低温效应。
因为单位加工气体产生的低温效应低，就要使用大量气体以产生气体分离装置要求的低温效应。例如，对于一个通过分离操作从空气（作为原料气）中提取氮气和氧气的装置，它必须有一道工序是将大量空气加压，然后送入该装置。这样就需要制造一个大加压器，将大量原料空气加压，结果是驱动加压器的能耗（一般情况下是电耗）增加了。大型设备和增加的能耗提高了由该气体分离装置生产（提取）氮气、氧气、氩气等产品气体时的费用，这是不利的。
本发明的一个主要目的是提出一种气体分离方法及其装置，当使用低温气体产生低温效应时能够提高单位气体流速产生的低温效应。
根据本发明一个方面，这里提出气体分离方法和小型且节能型的气体分离装置。
根据本发明另一方面，这里提出以低费用提取产品气体的气体分离方法和气体分离装置。
本发明的气体分离方法包括以下步骤：通过热交换器将原料气与低温气体进行热交换，以便使低温气体的温度回升;将热回升过的气体流入由膨胀涡轮提供能量的升压器中，使该气体加压;冷却加压后的气体至低温;将冷却至低温的气体流入上述膨胀涡轮，进行绝热膨胀;然后产生低温效应。
由下面参考附图的描述中可以明显看出来发明的其它目的和特征。
图1是描述本发明一个实施方案的流程图。
图2是描述本发明另一个实施方案的流程图。
图3是描述本发明又一个实施方案的流程图。
图4是描述本发明再一个实施方案的流程图。
下面通过实际的实施方案详述本发明。
参照图1，这是一个系统的流程图，说明了本发明用于提取氮气的设计装置。在本发明较好的实施方案中使用的原料气是空气。原料空气通过管道10，以8kg/cm2G的压力进入热交换器1。要注意的是，原料气中的水份和CO2通过预处理器（未示出）除去。进入热交换器1的原料空气与返回的氮气产品和低温废气进行热交换，然后冷却到饱和温度，其中部分气体被液化，通过管线11进入精馏塔2。在精馏塔2中，原料空气被分离成产品氮气和液态空气。由此分离出的氮气产品从精馏塔2的上部出来，由管线20进入热交换器1，其中氮气加热转变为正常温度。之后由管线21将氮气产品送出分离系统。氮气通过管线1转换的压力是7kg/cm2。液态空气从精馏塔2的下部出来并通过管线18。出来的液态空气由阀V1膨胀至压力约为3kg/cm2G，再由管线19进入氮气冷凝器3。精馏塔2中上升的氮气在氮气冷凝器3中液化，同时液态空气被汽化。由此汽化的低温废器由管线12排出。由管线12过来的低温废气在热交换器中回升到常温，该废气通过管线13在与膨胀涡轮5相连的升压器4中通过。升压器4的作用是将相当于涡轮5产生的低温效应的能量给予废气，使其温度和压力升高。就本说明书所及，该升压器带有一个压缩机、鼓风机或能使气体加压的设备。在这个实施方案中，升压器输出部分废气的压力是5kg/cm2G，温度从70℃至80℃，从升压器出来的废气在后接冷却器9中冷却到常温。水冷却器或者空气冷却器等均可做为后接冷却器。压力约为5kg/cm2G的冷却过的废气通过管线14再次进入热交换器1，进一步冷却到-120℃。然后从管线15排出。由管线15出来的低温废气流入膨胀涡轮5并在其中进行绝热膨胀，压力达0.3kg/cm2G，产生装置所需的低温效应。温度进一步降低的废气经过管线16进入热交换器1，冷却过的废气在其中回升至常温。随后，该废气由管线17排出系统。压力约为7kg/cm2G，温度为饱和温度的液氮产品从精馏塔2上部出来并由管线22排出系统。图中参数8表示低温绝缘槽。
根据本实施方案，从氮气冷凝器3排出的低温废气不是直接进入膨胀涡轮，而是在通过升压器加压后进入膨胀涡轮。因此，在膨胀涡轮进口处废气的压力可能超过从氮气冷凝器排放时废气的压力。对于膨胀涡轮，随着进口处压力增加，出口处压力减小，单位气体流速产生的热效应则增大，与先有技术比较，能够产生更大量的冷冻量。随着冷冻量增加，操作变得稳定，同时被提取的液氮产量亦增加。如果膨胀涡轮的鼓风机做为升压器，向鼓风机提供纯化的废气，则无需安装过滤器。另外，该鼓风机也不需要空气排出消声器，这是因为废气绝不会排放在鼓风机输出部分处的大气中。因此整个装置结构得到简化。由于废气基本不含水份或CO2，所以明显减少了膨胀涡轮的鼓风机的腐蚀，延长了该机的使用寿命。
上面描述了提取氮气装置的一个实施方案，但是本发明并不限定于此。本发明的装置有很宽范围的适用性。就是说，既可采用提取氧气和氮气的装置，也可采用设计用于提取氧气的装置。其它装置也是可采用的，用于低温过程的气体不仅包括废气，也包括产品气或原料气。
参照图2，这里描述了本发明另一个实施方案。图2是设计的从空气中提取氮气的系统流程图，采用与图1所示同样的分离操作。图1和图2两个实施方案之间一个很大的差别是当低温气体用来产生低温效应时，采用的是产品气-氮气。即N2（产品气）从精馏塔2出来由管线20（压力约为2.2kg/cm2G）进入热交换器1，在其中流过，温度回升到常温。随后，由管线13N2被送到升压器4，压力升至3.5kg/cm2G。在上述加压过程中温度升高的N2通过后接冷却器9冷却到常温，经管线14到热交换器1，其中N2再次被冷却，温度降到更低（约-120℃）。冷却过的N2经管线15进入膨胀涡轮5，绝热膨胀至压力约为0.3kg/cm2G，由此产生低温效应。低温N2由管线16进入热交换器1，通过其中的管道回升至常温。经由管线21，温度回升后的N2被送到所需之处。由图2所示的实施方案可见，如果低温效应高于需求的效应，为了防止整个系统不稳定，需要采用由管线23和阀V2，V3组合成的旁路。送入膨胀涡轮5的N2压力要用压力控制器（PC）30控制。
根据图2描述的实施方案，作为原料气的空气的压力在一般情况下最小可达3kg/cm2G，或该值左右，这个最小值是精馏所要求的。此外，在这个最小压力下，能够节省将原料空气加压时需要的能量。位于旁路上的压力控制器可使操作非常稳定。
本发明另一个实施方案下面参照图3除予描述。图3是从空气中通过分离操作提取氮气和氧气的装置的系统流程图，该实施方案采用的方法完全类似图1和图2所示的方式。其流程排列如下，低温气体通过热交换器1的媒介物升至常温;该常温气体再通过升压器4加压，然后由后接冷却器9冷却到常温;并且经管线14进入热交换器1，冷却至更低的温度;该气体再经管线15流入膨胀涡轮5，在其中绝热，产生低温效应。图2和图3两个实施方案之间明显的差别是部分原料气经管线27进入热交换器1，进行热交换，随后进入升压器4。这里原料气用做低温气体产生低温效应。该低温原料气在膨胀涡轮5内产生低温效应后通过管线28进入双精馏塔50的低压塔（上塔）。双精馏塔50的作用是从原料空气中提取氮气和氧气，并分别由管线20和25排出。随后，氧气和氧气在热交换器1中与原料空气进行热交换，回升温度。温度回升后的氧气通过管线26送到所需之处，氮气则通过管线21送到所需之处。双重精馏塔50的精馏过程是众所周知的，此处不予详述。
根据图3所示的实施方案，取出部分原料空气，以便由升压器加压，加压后的原料空气用来产生低温效应，这样单位气体流速产生的冷冻量增加。由于有此优点，减少产生低温效应需要的原料空气量以及降低电力消耗是可行的。
图4详细介绍了本发明另一实施方案。图4的方案基本与图1至图3所示方案相同。与前述方案相比，图4的改进不是下面所述，即当用从分离器60放出的低温气体产生低温效应时，将在主热交换器1中升温的气体送入升压器4。其改进在于，采用另一个辅助热交换器70，气体在其中升温后送到升压器4。而且，必须采用另一个不同的步骤，即当辅助热交换器70用于冷却气体时，该气体要提前由升压器4加压。
在图4的实施方案中，采用废气废为低温气体产生低温效应，但是使用产品气（N2或O2）和原料气做为另一种低温气体也是实际可行的，该低温气体可用于产生冷冻。在这种情况下，其管道布置与图2和图3的示意相同，所以在此略去描述。对于分离器60，可以采用图1至图3所示的精馏塔，但并不限定于此。例如可采用一种吸收类型的分离器，这类分离器借助于吸收剂（如沸石等）分离气体。
根据上述发明，在使用低温气体的过程中，通过低温过程增加单位低温气体流速的低温效能是可能的，这是节能和使装置小型化的主要之处。

Claims (14)

1、一种气体分离方法，该方法包括以下步骤：
采用热交换器，将过程中的低温气体与原料气进行热交换；
将热交换过的气体送入由膨胀涡轮驱动的升压器增加压力；
将加压后的气体冷却至低温；
将冷却至低温的气体送入膨胀涡轮，该气体在其中进行绝热膨胀，产生冷冻效应。
2、根据权利要求1的气体分离方法，其中所说过程中的低温气体是从精馏塔中分离出的废气。
3、根据权利要求1的气体分离方法，其中所说的低温气体是从所说精馏塔中分离出的产品气体。
4、根据权利要求1的气体分离方法，其中所说的低温气体是由所说热交换器冷却过的所说的部分原料。
5、根据权利要求2的气体分离方法，其中所说的废气在所说的膨胀涡轮中流动，进行绝热膨胀，由此产生所说的低温效应，再送入热交换器，与所说的原料气进行热交换，回升至常温，然后将该废气排出该过程。
6、根据权利要求3的气体分离方法，其中所说的气体产品被送入所说的膨胀涡轮，进行绝热膨胀，由此产生低温效应，再送入热交换器与原料气进行热交换，往该气体产品升至常温后排出。
7、根据权利要求4的气体分离方法，其中所说的原料气在膨胀涡轮中流动，进行绝热膨胀，由此产生低温效应，然后送入精馏塔，精馏分离出所说的原料气。
8、一种气体分离装置，该装置包括：
热交换器，用于将返回的低温气体进行热交换来冷却原料气;
精馏塔，用于将通过热交换器冷却下来的原料精馏分离成两种或两种以上的产品气体及废气，并分别排出所说的气体。
膨胀涡轮，用于将所说的低温气体进行绝热膨胀，产生低温效应;
通道，其作用是在将所说的低温气体用热交换器回升到常温后，将该常温气体导入由膨胀涡轮驱动的升压器;
冷却设备，用于将升压器加压过的气体冷却至更低的温度;
通道，用于将上述冷却设备冷却过的气体导入膨胀涡轮。
9、根据权利要求8的气体分离装置，其中的低温气体是从精馏塔分离出的废气。
10、根据权利要求8的气体分离装置，其中的低温气体是从精馏塔分离出的气体产品。
11、根据权利要求8的气体分离装置，其中的低温气体是部分由热交换器冷却过的原料气。
12、根据权利要求9的气体分离装置，其中有一条通道，在低温废气通过热交换器回升到常温后，该通道将该常温废气排出该过程，所说的低温废气在此之前借助于膨胀涡轮用来产生低温效应。
13、根据权利要求10的气体分离装置，其中在低温产品气体通过热交换器回升到常温后，有一条通道将该常温气体引入其需求处，该低温产品气体在此之前借助膨胀涡轮用来产生低温效应。
14、根据权利要求11的气体分离装置，其中有一条通道引导低温原料气进入精馏塔，该低温气体在此之前借助膨胀涡轮用来产生低温效应。
CN85109265.9A 1984-11-30 1985-11-27 从原料气中分离产品气体的方法及其装置 Expired CN1004229B (zh)

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