CN1058644A - 具有双产品侧冷凝器的低温空气分离系统 - Google Patents

具有双产品侧冷凝器的低温空气分离系统 Download PDF

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CN1058644A
CN1058644A CN91105316A CN91105316A CN1058644A CN 1058644 A CN1058644 A CN 1058644A CN 91105316 A CN91105316 A CN 91105316A CN 91105316 A CN91105316 A CN 91105316A CN 1058644 A CN1058644 A CN 1058644A
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tower
nitrogen
heat
exchange
equipment
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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，该系统将 加压后的原料空气至少部分冷凝，以蒸发高压液氮和 高压液氧，从而能在减少或不需要对产品进行压缩的 条件下制取高压氮气的高压氧气。

Description

本发明一般地涉及低温空气分离领域，更具体地说，涉及生产氧和氮的低温空气分离。
利用低温分离空气来制取氧和氮是一种已完善的工业方法。液体和蒸汽以逆流接触的方式流过一个塔或几个塔，氧和氮之间蒸汽压不同，使得氮富集于蒸汽中，而氧富集于液体中。由于存在蒸汽压差，分离塔中压力越低，就越容易使氧和氮分离。因此，通常是在压力较低的情况下最后分离产品氧和产品氮，所用压力常常只比大气压力高几磅/吋2。
人们常常希望得到高压产品氧和高压产品氮。在这种情况下，常用压缩机将产品压缩到所需要的压力。而产品压缩机压缩时的能源消耗及成本都是很昂贵的。
因此，本发明的一个目的是要提供一种改进的制取氧和氮的低温系统。
本发明的另一目的是要提供一种改进的制取氧和氮的低温系统，该系统能制取高压氧和高压氮，而又减少或不需要对产品气体进行压缩。
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，用本发明可完成上述任务和其它任务。本发明一方面包括：
一种制取氧和氮的低温空气分离方法，它包括：
（A）向高压塔供给原料空气，在高压塔内将原料空气分离成富氮蒸汽和富氧液体;
（B）使富氧液体从高压塔流入低压塔;
（C）冷凝富氮蒸汽以生产富氮液体，并将富氮液体送入低压塔;
（D）将流入低压塔的流体分离成富氮蒸汽和富氧液体;
（E）使富氧液体与原料空气进行间接热交换，以生产氧气产品;
（F）使富氮液体与原料空气进行间接热交换，以生产氮气产品。
本发明另一方面包括：
用于制取氧和氮的低温空气分离设备，它包括：
（A）热交换装置;
（B）从热交换装置到第一塔之间的管道装置;
（C）从第一塔到第二塔之间的管道装置;
（D）从第一塔到冷凝器/再沸器之间的管道装置;
（E）使流体从第二塔流到上述热交换装置的装置;
（F）使流体从冷凝器/再沸器流到上述热交换装置的装置。
在本说明书及权利要求书中所使用的术语“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，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  DistillationProcess）”。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。
蒸汽和液体接触分离过程取决于各组分的蒸汽压之差。蒸汽压大（或易挥发或低沸点）的组分容易富集于蒸汽相中，而蒸汽压小（或难挥发或高沸点）的组分容易富集于液相中。蒸馏是一种分离过程，它通过加热液体混合物使易挥发组分浓集于蒸汽相中，而使难挥发组份浓集于液相中。分凝是另一种分离过程，它通过冷却蒸汽混合物使易挥发组分浓集于蒸汽相中，而使难挥发组分浓集于液相中。精馏或连续蒸馏是通过逆流处理蒸汽相和液相，将逐次部分蒸发和部分冷凝结合起来的分离过程。蒸汽相和液相的逆流接触是绝热的，它可以包括不同相之间全部接触或局部接触。利用精馏原理分离混合物的分离工艺设备常常可互换地称之为“精馏塔”、“蒸馏塔”或“分馏塔”。
本说明书和权利要求书中所使用的术语“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，或者流体之间相互不掺混。
此处所用的术语“填料”指的是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。
此处所用的术语“冷凝器/再沸器”是指一种热交换装置，在该装置中，通过与正蒸发的塔底流体进行间接热交换来使蒸汽冷凝，并为该塔提供了上升的蒸汽流。
此处所用的术语“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。
此处所用的术语“透平膨胀”指的是让高压气体通过一个透平机而降低气体的压力和温度，从而产生冷量。常采用负载装置，例如发电机、功率计或压缩机之类来回收能量。
图1是本发明的方法和装置的优选实施例的示意图;
图2是本发明的方法和装置的另一优选实施例的示意图;
图3是本发明的方法和装置的再一个优选实施例的示意图。
下面将参照附图详细描述本发明的方法和装置。
参见图1，干净的、冷的、压缩过的原料空气1在热交换器30中与逆向回流进行间接热交换而被冷却，为了生产高压气体产品，原料空气的压力应足以使液体蒸发，这些将在下文中作更全面的描述。通常，原料空气的绝对压力范围为90-500磅/吋2（psia）。
原料空气被分成两部分，第一部分4可占原料气的5%-40%，它流经热交换装置31，该装置是一台双产品侧冷凝器。在热交换装置31中，空气部分4至少部分被冷凝，也可以全部被冷凝。然后，空气部分4经管道装置流入热交换器或过冷却器32中，并在其中过冷却。再流经阀33，最后作为流体6流入第一塔或高压塔34中，该塔是空分设备中双级塔系统的高压塔。高压塔34的运行压力范围一般为60-100磅/吋2。
原料空气的第二部分5可以占原料气的50%-90%，它经透平膨胀机35而被膨胀，以便为低温分离提供冷量。膨胀后的空气部分36流入高压塔34中。
原料空气的第三部分3可通过热交换器37与低压氮进行热交换而被冷却，再流经阀38，作为流体6的一部分进入高压塔34中。另外，若原料气部分4流经双产品侧冷凝器31时只部分被冷凝，未冷凝部分可以代替部分3或者加入部分3中，在热交换器37中进行热交换。
在高压塔34中，通过低温精馏，原料气被分离成富氧液体和富氮蒸汽。富氧液体9由管道装置送至热交换器66中，在该热交换器中，与低压氮气进行间接热交换而被冷却，然后进入第二塔或低压塔39中，该塔的运行压力低于高压塔34的运行压力，其范围一般为15-30磅/吋2。富氮蒸汽40从高压塔34经管道装置流入冷凝器/再沸器41中，与塔39的底部沉积物进行间接热交换而被冷凝。冷凝器/再沸器41虽然可设在塔的外部，但最好位于低压塔内部。所生成的富氮液体42流出冷凝器/再沸器41，其一部分43作为回流返回到高压塔34中。富氮液体8从高压塔34流出，经过热交换器66进入低压塔39。另一种方法是：也可以将液体42的一部分作为回流送至低压塔39中，以代替从高压塔34流出的流体8。
在低压塔39内，通过低温精馏，将送入塔内的流体分离成富氮蒸汽和富氧液体。富氮蒸汽10从低压塔39中流出，此低压氮顺次流过热交换器66、37和30而复热，并可作为低压氮气产品11被回收。富氧液体用于冷凝流体40中的富氮蒸汽，因而为低压塔39提供了上升的蒸汽流。
一部分富氧液体13从低压塔39中流出，进入双产品侧冷凝器31。在图1所示的优选的实施例中，为了制取高压氧气产品，将富氧液体增压，使其在双产品侧冷凝器中在较高压力下蒸发。再参见图1，富氧液体13经阀44流入至少一个贮槽中。如图1所示，富氧液体分别经阀47和48流入贮槽45和46中的一个或两个内，然后分别经阀49和50，再经阀51作为流体14进入过冷却器32中。上述一个或数个贮槽用于贮存液氧产品，以便事后作为产品氧送走。为了提高富氧液体的压力，可以在上述一个或数个贮槽上装备增压盘管或其它装置。或者也可以用液压泵或利用液压头，即液面之间的高度差来增加富氧液体的压力。增压后的富氧液体流经过冷却器32而被加热，所生成的流体52进入相分离器53中。从相分离器53流出的富氧液体54，流经双产品侧冷凝器31，在该冷凝器中，它被部分蒸发，而用于冷凝原料气，这在上面已讨论过。两相流17返回到相分离器53中，蒸汽55从相分离器53中流出，经热交换器30，作为高压氧气产品流18而被回收。高压氧气产品的压力范围可以达40-650磅/吋2。此外，根据所用系统的制冷情况，还可以回收一些液体产品。例如，除高压气体产品外，还可以生产液氧75和液氮76。
从冷凝器/再沸器41流出的富氮液体流入双产品侧冷凝器31中。在图1所示的优选的实施例中，使富氮液体增压，这样，在双产品侧冷凝器中，可在高压下蒸发富氮液体以生产高压氮气产品。再参见图1，富氮液体56通过阀57流入至少一个贮槽内。如图1所示，富氮液体分别经阀门60和61流入贮槽58和59中的一个或两个内，然后分别经过阀62和63进到过冷却器32中。上述一个或数个贮槽用于贮存液氮产品，以便事后作为产品氮送走。可以在上述一个或数个贮槽上装备增压盘管或其它装置，以使富氮液体增压。或者，也可以用液压泵或液压头来增加富氮液体的压力。增压后的富氮液体15流经过冷却器32而被加热，然后流经双产品侧冷凝器31而被蒸发，在冷凝器31中，富氮液体用于冷凝原料气，这在上面已讨论过。氮蒸汽流64流经热交换器30，然后作为高压氮气产品流65而被回收。高压氮气产品的压力范围可达100-600磅/吋2。
本发明的低温系统所制取的氮气纯度至少可为99%，甚至可高达99.99%或更高，所制取的氧气的纯度范围可为95%-99.95%。如果需要一些液氧和/或液氮，可以不经蒸发直接从塔中回收。当然，如果需要的话，也可以直接从塔中回收一些气态氧或气态氮。
图2表示本发明的另一个实施例，其中，原料空气的第一部分在流经双产品侧冷凝器之前先透平膨胀。图2中与图1相同的部件用相同标号表示，对这些部件将不再进行讨论。在图2所示的实施例中，将清洁的、冷的、经压缩的原料空气的第一部分70大约从热交换器30的中点抽出，然后经透平膨胀机71透平膨胀。所生成的原料气第一部分72流经热交换器31和32，并在透平膨胀机35的下游与原料气的第二部分汇合，而作为流体67流入高压塔34中。对于图2所示的实施例，这种附加的原料气透平膨胀，可以为塔提供额外的冷量，这样可使液体产品的产量增加。而气态产品仍可在低压下制取。
图3表示本发明的又一个实施例，其中，将原料气第一部分的一支透平膨胀，再流经一个分开的侧冷凝器，在该冷凝器中该部分原料气与富氮液体进行热交换。图3中与图1相同的部件用相同标号表示，在此对这些部件不再进行讨论。
在图3所示的实施例中，从热交换器30中点附近抽出清洁、冷的、压缩过的原料气的第一部分的支流80，使其通过透平膨胀机81而透平膨胀。所生成的原料气支流82流经热交换器83和阀84，再与流经热交换器68和69的原料气第一部分的第二支85汇合而形成流体部分4，使该部分流入高压塔34。在热交换器83中的热交换是与富氮液体15之间进行的，之后，富氮液体15流经热交换器30，并作为高压氮气产品而被回收。因此，在图3所示的实施例中，双产品侧冷凝器为两部分，即热交换器68和83。利用图3所示的实施例，人们可以制取两种压力各不相同的产品。而且，利用图3所示的实施例所制取的液体产品，尽管不能象图2所示的实施例那么多，但却比图1所示的实施例要多。
高压塔和低压塔中之一或二者内可以装有塔盘或填料。如果充装填料，可以采用无规填料或结构定形填料。但是本发明特别适合在塔内充装结构定形填料，因为填料能降低塔内运行压力，有助于提高产品回收率并能增加液体产量。填料塔还可增加一些附加段，而不会显著增高塔的运行压力。由于结构定形填料的性能更易预测，而且在给定床高的情况下段数更多，所以结构定形填料比无规填料更好。这对于系统的初次投资及系统的组成都是很重要的。
表Ⅰ列出了利用图1的实施例对本发明进行计算机模拟的数据总结。表Ⅰ中的数据只是为了用图表说明本发明，并不意味着限制本发明，表Ⅰ中的流体标号与图1中的流体标号相同。
表Ⅰ
流体号  温度  压力  流量  浓度（摩尔百分比）
（°F） （磅/吋2） （MCFH） N2O2
1  44  126  1000  78  21
4  -252  125  265  78  21
5  -252  125  713  78  21
6  -282  82  287  78  21
36  -273  82  713  78  21
8  -289  79  382  99  1
9  -282  82  618  65  33
10  -316  19  770  98  1
11  43  15  770  98  1
56  -288  79  30  100  0
65  43  135  20  100  0
13  -290  22  200  0  99.6
18  43  45  193  0  99.6
75  -290  45  7  0  99.6
76  -288  79  10  100  0
虽然我们结合一些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 (24)

1、一种制取氧和氮的空气分离方法，包括：
(A)向高压塔提供原料空气，在高压塔内将原料空气分离成富氮蒸汽和富氧液体；
(B)将富氧液体从高压塔送至低压塔；
(C)冷凝富氮蒸汽，以生产富氮液体，将富氮液体送至低压塔；
(D)将流入低压塔中的流体分离成富氮蒸汽和富氧液体；
(E)使富氧液体与原料空气进行间接热交换，以制取氧气产品；
(F)使富氮液体与原料空气进行间接热交换以制取氮气产品。
2、如权利要求1所述的方法，其特征是将原料空气分成第一部分和第二部分，通过步骤（E）和（F）中的热交换，使第一部分至少部分冷凝。
3、如权利要求2所述的方法，其特征是通过步骤（E）和（F）中的热交换，使原料空气的第一部分全部冷凝。
4、如权利要求2所述的方法，其特征是第二部分进入高压塔之前使其透平膨胀。
5、如权利要求1所述的方法，其特征是还包括回收从低压塔中取出的富氮蒸汽。
6、如权利要求1所述的方法，其特征是通过与富氧液体进行间接热交换而冷凝富氮蒸汽。
7、如权利要求1所述的方法，其特征是在进行步骤（E）的热交换之前，使富氧液体增压。
8、如权利要求1所述的方法，其特征是在进行步骤（F）的热交换之前，使富氮液体增压。
9、如权利要求2所述的方法，其特征是在进行步骤（E）和（F）的热交换之前，使原料空气的第一部分透平膨胀。
10、如权利要求2所述的方法，其特征是将原料空气的第一部分分成第一支和第二支，将第一支透平膨胀然后进行步骤（F）的热交换，将第二支进行步骤（E）的热交换。
11、如权利要求1所述的方法，其特征是还包括回收一些富氧液体。
12、如权利要求1所述的方法，其特征是还包括回收一些富氮液体。
13、用于制取氧和氮的低温空气分离设备，它包括：
（A）热交换装置;
（B）从热交换装置到第一塔之间的管道装置;
（C）从第一塔到第二塔之间的管道装置;
（D）从第一塔到冷凝器/再沸器之间的管道装置;
（E）使流体从第二塔流到上述热交换装置的装置;
（F）使流体从冷凝器/再沸器流到所述热交换装置的装置。
14、如权利要求13所述的设备，其特征是使流体从第二塔流到热交换装置的装置包括至少一个贮槽。
15、如权利要求13所述的设备，其特征是使流体从冷凝器/再沸器流到热交换装置的装置包括至少一个贮槽。
16、如权利要求13所述的设备，其特征是使流体从第二塔流到热交换装置的装置包括一个液压泵。
17、如权利要求13所述的设备，其特征是使流体从冷凝器/再沸器流到热交换装置的装置包括一个液压泵。
18、如权利要求13所述的设备，其特征是还包括一个与第一塔流体流动相通的透平膨胀机。
19、如权利要求13所述的设备，其特征是还包括设在从热交换装置到第一塔的管路上的过冷却器装置。
20、如权利要求13所述的设备，其特征是还包括一个与热交换装置流体流动相通的透平膨胀机。
21、如权利要求13所述的设备，其特征是上述热交换装置包括第一部分和第二部分，部分（E）中装置的通道装置用于使流体流到上述热交换装置的第二部分，部分（F）中装置的通道装置用于使流体流到上述热交换装置的第一部分。
22、如权利要求21所述的设备，其特征是还包括一个与上述第二部分流体流动相通的透平膨胀机。
23、如权利要求13所述的设备，其特征是第一塔内部至少部分区域充装有结构定形填料。
24、如权利要求13所述的设备，其特征是第二塔的内部至少部分区域充装有结构定形填料。
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CN102538397A (zh) * 2012-01-18 2012-07-04 开封黄河空分集团有限公司 一种由空气分离制取氮气或制取氮气同时附产氧气的工艺
CN105229400A (zh) * 2013-04-25 2016-01-06 林德股份公司 从带有临时储存器的空气分离系统中获取空气产品的方法以及空气分离系统
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CN108529804A (zh) * 2018-04-24 2018-09-14 浙江荣凯科技发展有限公司 一种二氯烟酸生产污水处理装置

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DE69103347D1 (de) 1994-09-15
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DE69103347T3 (de) 1999-02-25
BR9102694A (pt) 1992-02-04
ES2057671T5 (es) 1998-11-01
KR960003271B1 (ko) 1996-03-07
KR920000363A (ko) 1992-01-29
DE69103347T2 (de) 1995-03-16
EP0464630A1 (en) 1992-01-08
EP0464630B2 (en) 1998-09-09
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CA2045739A1 (en) 1991-12-28
EP0464630B1 (en) 1994-08-10
US5148680A (en) 1992-09-22

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