CN1226672A - 生产低纯氧和高纯氮的低温混杂系统 - Google Patents

生产低纯氧和高纯氮的低温混杂系统 Download PDF

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CN1226672A
CN1226672A CN97122517A CN97122517A CN1226672A CN 1226672 A CN1226672 A CN 1226672A CN 97122517 A CN97122517 A CN 97122517A CN 97122517 A CN97122517 A CN 97122517A CN 1226672 A CN1226672 A CN 1226672A
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nitrogen
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H·E·霍华德
D·P·博纳奎斯特
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Praxair Technology Inc
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Abstract

以高的产品回收率同时生产低纯氧和高纯氮的混杂系统,其中来自吸附剂系统的解吸流出物送入低温精馏塔,并且优选来自所述塔的底部流体为所述吸附剂系统提供附加的进料。

Description

生产低纯氧和高纯氮的低温混杂系统
本发明总的涉及空气的分离，更具体地说，涉及进料空气的分离以生产低纯氧和高纯氮。
在一些工业应用上需要同时使用低纯氧和高纯氮。如在玻璃制造上，在含氧燃料燃烧时使用低纯氧来加热和熔化制造物料，而高纯氮则用作焙融玻璃的惰性气氛。一般在这种情况下，氮对氧的产品流的要求比率为1.5至2.0。
通过空气的低温精馏可有效地生产高纯氮和低纯氧，但如没有昂贵的方法改良，则在所需的比率范围内得不到高的产品回收率。
因此，本发明的一个目的是提供可同时有效地生产低纯氧和高纯氮的低温精馏系统。
本发明的另一个目的是提供对两种产品可以高的产品回收率有效地生产低纯氧和高纯氮的低温精馏系统。
对本领域技术人员而言，在阅读了本说明书后显而易见的上述及其它目的可通过本发明得到实现，本发明的一方面是：
一种生产低纯氧和高纯氮的方法，包括：
(A)将进料空气送进包含至少一个吸附床的吸附剂系统，并在该吸附剂系统内将氮从进料空气中吸附出来以制得富氧蒸气和富氮蒸气；
(B)将富氧蒸气作为产品低纯氧回收；
(C)将富氮蒸气送入一塔中并通过在该塔内低温精馏将该富氮蒸气分离成氮顶部流体和含氧底部流体；和
(D)将氮项部流体作为产品高纯氮回收。
本发明的另一方面是：
生产低纯氧和高纯氮的设备，包括：
(A)包含至少一个吸附床的吸附剂系统，并具有进料输入装置，藉此将进料空气送入该吸附剂系统中；
(B)用于从吸附剂系统中回收低纯氧的装置；
(C)用于将来自吸附剂系统的富氮蒸气送入低温精馏塔的装置；和
(D)将来自低温精馏塔上部的流体作为产品高纯氮回收的装置。
此处所用的术语“进料空气”意指主要包括氧和氮的混合物，如环境空气。
此处所用的术语“低纯氧”意指氧浓度在50-98.5％(摩尔)范围内的流体。
此处所用的术语“高纯氮”意指氮浓度高于98.5％(摩尔)的流体。
此处所用的术语“塔”意指蒸馏塔或分馏塔或区，即接触塔或区，其中液相和气相逆流接触以完成流体混合物的分离，如通过气相和液相在一系列安置于塔内的垂直放置塔盘或塔板和/或在如结构或无规填料的填料单元上接触。对蒸馏塔的进一步讨论，请参见《化学工程师手册》，第5版，R.H.Perry和C.H.Chilton编，Mc Graw-Hill BookCompany出版，纽约，第13段，“连续蒸馏法”。
气液接触分离法基于各组分蒸气压的不同。高蒸气压(或易挥发或低沸点)组分易于浓缩在气相而低蒸气压(或难挥发或高沸点)组分易于浓缩在液相中。精馏或连续蒸馏是一种结合由气液相的逆流处理获得的连续部分蒸发和冷凝的分离方法。气液相的逆流接触通常是绝热的，并可包括各相之间的积分(阶段的)或微分(连续的)接触。利用精馏原理以分离混合物的分离法设备常可互换地称为精馏塔、蒸馏塔或分馏塔。低温精馏是至少部分在温度等于或低于150度开尔文(°K)下进行的精馏法。
此处所用的术语“间接热交换”意指流体之间在没有任何物理接触或混合的情况下将两种流体流导入热交换关系。
此处所用的术语“顶部冷凝器”意指从塔蒸气中产生塔下流液体的热交换设备。
此处所用的术语“汽轮膨胀”和“汽轮骤冷器”分别意指高压气流通过汽轮机以降低气体的压力和温度藉以产生制冷作用的方法和设备。
此处所用的术语“上部”和“下部”意指分别经于塔中点以上和以下的塔的部分。
此处所用的术语“吸附剂”意指可在其间隙或微孔内接受或捕获气体或流体种类的物质(通常为固体)。吸附剂的例子包括矾土、氧化硅、碳和分子筛。特别优选的吸附剂是氮选择性分子筛。
此处所用的术语“吸附床”意指吸附剂颗粒邻近相互之间的汇集体并构成可被流体所接触的形式。
唯一的附图是本发明低温混杂进料空气分离系统的一优选实施方案的示意图。
本发明使得人们可以高的产品回收率有效地生产两种产品：高纯氮和低纯氧，特别是氮对氧的产品比率在1.5-2.0范围内。本发明使用了一吸附系统和一低温精馏系统。来自低温精馏塔的底部流体优选循环至吸附系统，并在该吸附系统中进行分离。
本发明将参见附图作极详尽的描述。现参照附图，进料空气25通过压缩机1而被压缩至压力一般在10-100磅/平方英寸(绝对压)，所得进料空气流26被送入包含至少一个吸附床的吸附剂系统2。图中所示的吸附剂系统2包含二个吸附剂床，并且操作时，当一个床的吸附剂正变得负荷时，流26从该床循环至另一床。吸附在一个床进行而解吸在另一床进行，当吸附床变得负荷时，各流动将为逆流。一般与多床吸附剂系统常在一起的管道和阀门不示于图上。本领域技术人员熟悉多床吸附系统及其操作。
在吸附剂系统内进料空气流26的氮被优先吸附到包含吸附床的吸附剂颗粒上，得到富氧蒸气。氧浓度优选在80-95％(摩尔)范围内的富氧蒸气以流27从吸附剂系统2中导出，送入缓冲罐3中，并从中以流19作为产品低纯氧回收。
当吸附剂系统2的一个床变得为氮所满负荷时，通过如将该床暴露在通过真空泵4所造成的真空条件下进行解吸。该吸附剂系统可直接解吸至环境压力而不需真空泵。解吸令已吸附到吸附剂颗粒上的氮形成富氮蒸气，被从吸附剂系统中以流18导出。
氮浓度一般在85-95％(摩尔)的富氮流18通过真空泵4进入缓冲罐5。从缓冲罐5中富氮流流经压缩机6被压缩至压力一般在50-200磅/平方英寸(绝对压)的范围，然后通过冷却器7冷却压缩热。此后该富氮蒸气流流经高沸点吸附剂系统8，在图示的该实施方案中，该吸附剂系统是类似于氮吸附剂系统2的二床系统。通过流经吸附剂系统8，富氮蒸气被除去高沸点杂质如二氧化碳、水蒸气和各种碳氢化合物。
洁净、受压的富氮蒸气28被送入主换热器9，在其中通过与各回流进行间接热交换而被冷却。富氮蒸气流28的第一部分29部分横过换热器9后被导出，并通过汽轮骤冷器10而被汽轮膨胀以产生制冷作用。所得汽轮膨胀流30被送入塔11中。富氮蒸气流28的第二部分31完全横过主换热器9，并通过阀13得到节流，送入塔11中。
塔11在压力一般为30-180磅/平方英寸(绝对压)的范围内操作。塔11内富氮蒸气通过低温精馏被分离成氮顶部流体和含氧底部流体。氮顶部流体作为蒸气流32从塔11的上部导出。氮蒸气流32的一部分33通过主换热器9而被加热，所得流16作为产品高纯氮回收。如需要，流33可在进入换热器9之间进行汽轮膨胀以产生制冷作用。氮蒸气流32的另一部分34被送入顶部冷凝器12，在其中通过与含氧底部流体进行间接热交换而被冷凝。所得氮液以流35从顶部冷凝器12中导出。流35的至少一部分36作为回流被送入塔11中。如需要，来自顶部冷凝器12的氮流体的一部分37可通过阀15并作为产品高纯氮液体回收。
含氧底部流体以流38从塔11的下部导出，经阀14节流并送入顶部冷凝器(2)，在其中蒸发以进行前述氮顶部流体的冷凝。如需要，流38可在被送入顶部冷凝器12之前与流33和/或39进行间接热交换而得到低温冷却。所得含氧蒸气以流39从顶部冷凝器12中导出，并通过换热器9得到加热，生成可从系统中除去的含氧底部流体流40。如需要，流39可在送入换热器9之前汽轮膨胀以产生制冷作用。
附图示意了本发明的一优选实施方案，其中含氧底部流体的部分或全部通过所述系统得到循环。由于送入塔11内的进料的特性及所述塔的操作，含氧底部流体具有和空气的氧浓度不相上下的氧的浓度，一般在15-25％(摩尔)的范围内，一般为约21％(摩尔)。这使得含氧流40可被送入吸附剂系统2中进行分离以生产富氧蒸气和富氮蒸气。
参照回附图，含氧底部流体流40可被分为流17和流41。流41通过换热器42而得到加热，并用于清扫或解吸高沸点吸附剂系统8。或者氮流33的一部分也可用来清扫或解吸高沸点吸附剂系统8。所得流43离开所述系统。如需要，若含氧底部流体所含的氧浓度高于空气的氧浓度，则部分流43可如图所示通过虚线44与流17重新汇合。
在附图所示的实施方案中，流17被送入压缩机1，在其中与进料空气25汇合形成流26被送入吸附剂系统2，并如前述般进行处理。
虽然本发明已参照特定优选实施方案做了详细的描述，本领域技术人员将会理解到在权利要求书的精神和范畴内本发明的其它实施方案。

Claims (10)

1．生产低纯氧和高纯氮的方法，包括：
(A)将进料空气送进包含至少一个吸附床的吸附剂系统，并在该吸附剂系统内将氮从进料空气中吸附出来以制得富氧蒸气和富氮蒸气；
(B)将富氧蒸气作为产品低纯氧回收；
(C)将富氮蒸气送入一塔中并通过在该塔内低温精馏将该富氮蒸气分离成氮顶部流体和含氧底部流体；和
(D)将氮顶部流体作为产品高纯氮回收。
2．权利要求1的方法，还包括将含氧底部流体送入所述吸附剂系统中，以进一步生产富氧蒸气和富氮蒸气。
3．权利要求1的方法，其中将富氮蒸气在送入所述塔之前进行压缩。
4．权利要求1的方法，其中富氮蒸气在送入所述塔之前被清除各种高沸点杂质。
5．权利要求1的方法，其中富氮蒸气在送入所述塔之前被冷却，并且至少一部分富氮蒸气被汽轮膨胀。
6．生产低纯氧和高纯氮的设备，包括：
(A)包含至少一个吸附床的吸附剂系统，并具有进料输入装置，藉此将进料空气送入该吸附剂系统中；
(B)用于从吸附剂系统中回收低纯氧的装置；
(C)用于将来自吸附剂系统的富氮蒸气送入低温精馏塔的装置；和
(D)将来自低温精馏塔上部的流体作为产品高纯氮回收的装置。
7．权利要求6的设备，还包括将来自所述塔下部的流体送入所述吸附剂系统的进料输入装置的装置。
8．权利要求6的设备，其中将来自所述吸附剂系统的富氮蒸气送入所述低温精馏塔的装置包括一压缩机。
9．权利要求6的设备，其中将来自所述吸附剂系统的富氮蒸气送入所述低温精馏塔的装置包括用于从所述富氮蒸气中除去高沸点杂质的第二吸附剂系统。
10．权利要求6的设备，其中将来自所述吸附剂系统的富氮蒸气送入所述低温精馏塔的装置包括一个汽轮骤冷器。
CN97122517A 1997-01-07 1997-10-31 生产低纯氧和高纯氮的低温混杂系统 Pending CN1226672A (zh)

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