CN1198524A - 生产高压氮和高压氧的低温精馏系统 - Google Patents

生产高压氮和高压氧的低温精馏系统 Download PDF

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CN1198524A
CN1198524A CN98105766A CN98105766A CN1198524A CN 1198524 A CN1198524 A CN 1198524A CN 98105766 A CN98105766 A CN 98105766A CN 98105766 A CN98105766 A CN 98105766A CN 1198524 A CN1198524 A CN 1198524A
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D·P·波纳奎斯特
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Abstract

用于加工进料空气的低温精馏系统,其中一定义的大流量高压氮架蒸汽直接从双塔的高压塔中回收,迎着进料空气的一部分蒸发加压的氧液体以生产高压氧产品,将所得的冷凝进料空气部分以定义的方式分流并送入双塔的每个高压塔和低压塔中。

Description

生产高压氮和高压氧的低温精馏系统
本发明总的涉及空气的低温精馏，更具体地涉及空气的低温精馏以生产高压氮和高压氧。
低温精馏诸如空气的混合物以生产氧和氮是已经很成熟的工业方法。将液体和蒸汽通过一个或多个塔逆流接触，氧和氮的蒸汽压差使得氮富集于蒸汽中而氧富集于液体中。由于蒸汽压差，分离塔中的压力越低，分离成氧和氮就越容易。因此，一般在较低的压力下(通常仅比环境压力高几个磅/平方英寸(psi))进行最终分离成产品氧和氮。
在高压下有时同时需要产品氧和产品氮。在这些情况下氧蒸汽和蒸气在压缩机中被压缩至所需的压力。根据用于产品压缩机的能量费用和基本投资而言该压缩过程是昂贵的。
因此，本发明的一个目的是提供用于生产高压氮和高压氧而无需产品气体压缩的低温精馏系统。
本领域技术人员阅读完本公开后显而易见的上述及其它目的可由本发明来实现，本发明一方面是：
通过进料空气的低温精馏生产高压氮和高压氧的方法，它包括：
(A)将总进料空气的一部分冷凝以制得冷凝的进料空气，将冷凝的进料空气的第一部分送入高压塔，将占总进料空气5-17.5％的冷凝的进料空气的第二部分送入低压塔；
(B)在高压塔内通过低温精馏生产富氮蒸汽和富氧液体，并将至少占总进料空气20％的富氮蒸汽的一部分作为高压氮回收；
(C)在低压塔内通过低温精馏生产富氮蒸汽和富氧液体；
(D)将富氧液体从低压塔中导出，加压所导出的富氧液体以制得高压富氧液体，并通过与所述冷凝的进料空气进行间接热交换而蒸发该高压富氧液体以产生高压富氧蒸汽；和
(E)将高压富氧蒸汽作为高压氧回收。
本发明的另一方面是：
通过低温精馏进料空气生产高压氮和高压氧的设备，包括：
(A)包含第一塔、第二塔以及产品锅炉换热器的低温精馏设备；
(B)将进料空气送入产品锅炉换热器的装置，将进料空气从产品锅炉换热器送入第一塔的装置，以及将占总进料空气5-17.5％的进料空气从产品锅炉换热器中送入第二塔的装置；
(C)将至少占总进料空气20％的、来自第一塔上部的流体作为高压氮回收的装置；
(D)一台液体泵，将液体从第二塔下部送往液体泵的装置，以及将液体从液体泵送往产品锅炉换热器的装置；和
(E)将来自产品锅炉换热器的液体作为高压氧回收的装置。
此处所用的术语“进料空气”指主要包括氧气、氮气和氩气如环境空气的混合物。
此处所用的术语“总进料空气”指所有被送入系统中进行低温精馏的进料空气。
此处所用的术语“塔”指蒸馏或分馏塔或区，即接触塔或区，其中液相和气相逆液接触以实现流体混合物的分离，例如通过气相和液相在塔内一系列垂直放置的塔盘或塔板和/或诸如结构填料或无规填料的填料单元上接触来实现。对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，Mc Graw-HillBook Company出版，纽约，第13章，“连续蒸馏法”。术语“双塔”用来意指高压塔上部与低压塔下部发生热交换关系。双塔的进一步讨论见于Ruheman的《气体分离》，牛津大学出版社，1949年，第VII章，“工业气体分离”。
气体和液体接触分离法基于各种组分的蒸汽压差。高蒸气压(或易挥发或低沸点)组分易于富集于气相而低蒸气压(或难挥发或高沸点)组分易于富集于液相。部分冷凝是利用蒸汽混合物的冷却来富集气相中的挥发组分从而难挥发组分留在液相中的分离方法。精馏或连续蒸馏是通过气液相的逆流处理获得连续部分蒸发和部分冷凝的分离方法。气液相的逆流接触一般是绝热的，并可包括各相之间的积分(阶段)或微分(连续)接触。利用精馏的原理来分离混合物的分离法设备通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不超过150°K下进行的精馏方法。
此处所用的术语“间接热交换”指在流体相互之间没有任何物理接触或混合的情况下将两种液流导入热交换关系。
此处所用的术语“顶部冷凝器”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“汽轮膨胀和冷凝骤冷器”分别指用于高压气体流经汽轮机以减少压力及气体的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”指分别位于塔的中点以上和以下的塔的部分。
此处所用的术语“平衡段”指气-液接触段，在其中离开该段的蒸汽和液体达到传质平衡，例如具有100％效率的塔盘或一填料单元高度相当于一理论塔板(HETP)。
此处所用的术语“氩气塔”指加工含有氩有的进料并制得产品氩气浓度超过进料氩气浓度的塔。
图1是本发明一个优选实施方案的示意说明。
图2是本发明另一个优选实施方案的示意说明。
图3是本发明再一个优选实施方案的示意说明。
图4是本发明所定义的优选产品高压氮部分的优点的图解说明。
图5是本发明所定义的液体空气分配的优点的图解说明。
本发明包括发现当低温精馏系统内的推动力被减少到氧的回收率开始对推动力的进一步减少变得敏感的那个点时，在低温精馏设备中将出现用于生产氧的最小分离能，而且这将发生于氧的回收率不超过约98％。高压氮从高压塔中导出并回收，这与氧的回收率为约97％相一致。另外，通过使盘架蒸汽即在特定值的氧回收率下可得到的高压氮的数量达到最大，高压塔和低压塔之间液体进料空气的最佳分布使氧分离能达到最小。通过蒸发加压的氧产品产生液体进料空气，同时使氧分离能达到最小的液体进料空气的最佳分布也是使氩回收率达到最大的相同分布。
本发明将参照附图作更详尽的讨论。现参见图1，作为本发明系统总进料空气的进料空气60通过基础负荷压缩机30被压缩至绝对压力一般在80-250磅/平方英寸(绝对压)(psia)的范围内，然后被压缩的进料空气61流经预净化器50除去诸如二氧化碳、水蒸汽和碳氢化合物的高沸点杂质。已去杂质的压缩进料空气62被分成进料空气流64和进料空气流63。流64通过与汽轮骤冷器32连接的增压压缩机31被升压。压缩机31的流出物96部分流经主换热器1，在其中通过与各种回流进行间接热交换而得到冷却。所得冷却的进料空气从主换热器1以流97送至汽轮骤冷器32，在其中被汽轮膨胀以产生制冷作用。然后所得已汽轮膨胀的进料空气流98从汽轮骤冷器32送入第二或低压塔11中。
进料空气流63被分成流65和流66。流65通过流经主换热器1被冷却，所得的冷却进料空气流67被送入第一或高压塔10，高压塔10是双塔的高压塔，在压力一般为75-100psia的范围内操作。流66通过流经增压压缩机33被压缩至压力一般在100-600psia的范围内，所得加压的进料空气68通过流经主换热器1得到冷却，随后通过与加压的液氧进行间接热交换在产品锅炉换热器中得到冷凝以制得冷凝的进料空气。该冷凝的进料空气占总进料空气60的约15-40％(摩尔)。
在示于图1的本发明实施方案中，加压的进料空气68通过流经主换热器1得到冷却，所得的冷却进料空气以流69被送至产品锅炉22，在其中被冷凝。所得冷凝进料空气70被分成第一部分71和第二部分72。包含25-75％冷凝进料空气70的第一部分71被送入高压塔10中。包含25-75％冷凝进料空气流70的第二部分72通过部分横过过热器2得到低温冷却，所得低温冷却的进料空气流99经阀100在塔11顶部下5-15个平衡段的位置被送入低压塔11中。第二部分72占总进料空气的5-17.5％、优选7.5-15％、最优选10-12.5％。
高压塔10内通过低温精馏进料空气被分离成富氮蒸气和富氧液体。富氮蒸汽作为流74从高压塔10的上部导出并分成部分109和部分75。部分109通过流经主换热器1得到加热并在压力一般在75-99psia的范围内以及氮的浓度至少为98％(摩尔)作为产品高压氮110回收。产品高压氮包含至少20％(摩尔)、优选约20-35％(摩尔)的总进料空气流60。富氮蒸汽部分75被送入主冷凝器20，在其中通过与低压塔11的底部液体进行间接热交换而得到冷凝。所得富氮液体76被分成作为回流返回高压塔10的部分77和通过部分横过过热器2而得到低温冷却的部分78。所得低温冷却流79经阀81被送入低压塔11中。如需要，流79的部分123可送经阀122并作为高压液氮回收。
氧浓度一般在25-45％(摩尔)的富氧液体作为流73从高压塔10的下部导出，通过部分横过过热器2而得到低温冷却，并分成第一部分83和第二部分86。第一部分83经阀84被送入低压塔11。第二部分86经阀87被送入氩气塔塔顶冷凝器21，在其中第二部分86基本全部被蒸发。所得富氧蒸汽以流89从塔顶冷凝器21经阀90在流83被送入低压塔11的进塔点下1-10个平衡段的位置被送入低压塔11中。本领域技术人员将意识到，出于安全上的原因，不超过0.3％送入氩气塔塔顶冷凝器的富氧液体的少量液体排水可从该塔顶冷凝器的底部导出。
第二或低压塔11是也包括高压塔10的双塔的低压塔，在低于高压塔10的压力、一般在16-24psi下操作。低压塔11内各种进入该塔的进料通过低温精馏被分离成富氮蒸汽和富氧液体。富氧蒸汽作为流106从低压塔11的上部导出，通过流经过热器2和主换热器1而得到加热，并以流108从系统中导出，它可作为氮浓度至少为98％(摩尔)的低压气态氮回收。
富氧液体以流102从低压塔11的下部导出，并被加压以生产压力一般在25-500psia范围内的高压富氧液体。在示于图1的本发明实施方案中，通过将流102送经液体泵34来获得加压以制得高压富氧液体103。流103被送入产品锅炉22，在其中通过与上述冷凝的进料空气进行间接热交换而至少部分被蒸发。如需要，一些富氧液体可以流119从产品锅炉22中导出，流经阀120并作为液体氧产品121回收。被蒸发的富氧液体以流104从产品锅炉22中导出，通过流经主换热器1被加热，并作为压力一般在25-500psia范围内以及氧浓度一般在98-100％(摩尔)范围内的高压氧产品105回收。
主要包含氧和氩的汉以流117从低压塔11被送入氩气塔12，在其中通过低温精馏被分离成富氩蒸汽和富氧液体。富氧液体以流118从氩气塔12被送入低压塔11中。富氩蒸汽以流111被送入塔顶冷凝器21，在其中通过与上述蒸发的富氧液体进行间接热交换而得到冷凝。所得富氩液体以流112被送入塔顶冷凝器21。流112的一部分116作为回流被送入氩气塔12。流112的另一部分113被送往阀114并作为氩气浓度一般在90-99％范围内的粗制氩产品115回收。
图4显示了氧的相对分离能与作为高压氮产品回收的总进料空气的部分的关系。当产品高压氮的分数达到约20％时用于氧生产的相对分离能达到一低的水平，并当高压氮产品分数超过20％时仍保持在该低的水平上。当出现低的能量水平时氧的回收率只降至约97％。该图也显示了氩的回收率。
图5给出了液体进料空气在高压塔及低压塔之间分流的最优化方案。图5表明，当高压氮产品分数为至少20％进料空气时，在所定义的液体空气分布到本发明的低压塔中氧的回收率达到最大。这在高压氮产品分数低于20％进料空气时并不出现。实际上当高压氮产品回收率低于20％进料空气时，最大限度地减少或者甚至取消液体空气流向低压塔更为有利。
图2和图3分别显示了本发明两个优选实施方案。对于各普通单元图中的数字的含义是一样的，因此这些普通单元将不再次详述。
在示于图2的实施方案中，被压缩的进料空气61首先被送至增压压缩机31，所得压缩的进料空气流162被送经预净化器50。所得进料空气流163通过流经主换热器1而得到冷却，所得冷却的进料空气流164被分成如示于图1实施方案中所述在产品锅炉22中冷凝的第一部分165，以及通过流经汽轮骤冷器32而得到汽轮膨胀以产生制冷作用然后作为流167被送入高压塔10中的第二部分166。
在示于图3的实施方案中，产品锅炉换热器为主换热器的一部分而不是图1和图2所示的实施方案中的单独的产品锅炉。现参见图3，进料空气流163被分成第一部分175和第二部分176。第一部分175通过流经主换热器1而得到冷却，所得冷却进料空气流177通过流经汽轮骤冷器32而被汽轮膨胀以产生制冷作用，然后作为流178被送入高压塔10中。第二部分176通过流经压缩机32加压，并且所得压缩的流179通过迎着蒸发的加压富氧液体流经主换热器1而得到冷凝以制得如前述般进一步加工的冷凝进料空气流70。如需要，液体氧产品121从液体泵34的上流流102中回收，而加压的富氧液体103被送经主换热器1，在其中被蒸发以生产高压氧产品105。
现在通过利用本发明，通过进料空气的低温精馏而无需产品气体的压缩，我们可以有效地同时生产处于高压的氧和氮。虽然本发明已参照特定的优选实施方案作了详述，但本领域技术人员将意识到包括在权利要求的精神和范围内还有本发明的其它实施方案。

Claims (9)

1.通过进料空气的低温精馏生产高压氮和高压氧的方法，它包括：
(A)将总进料空气的一部分冷凝以制得冷凝的进料空气，将冷凝的进料空气的第一部分送入高压塔，将占总进料空气5-17.5％的冷凝的进料空气的第二部分送入低压塔；
(B)在高压塔内通过低温精馏生产富氮蒸汽和富氧液体，并将至少占总进料空气20％的富氮蒸汽的一部分作为高压氮回收；
(C)在低压塔内通过低温精馏生产富氮蒸汽和富氧液体；
(D)将富氧液体从低压塔中导出，加压所导出的富氧液体以制得高压富氧液体，并通过与所述冷凝的进料空气进行间接热交换而蒸发该高压富氧液体以产生高压富氧蒸汽；和
(E)将高压富氧蒸汽作为高压氧回收。
2.权利要求1的方法，其中所回收的高压氮占总进料空气的20-35％。
3.权利要求1的方法，其中所冷凝的进料空气占总进料空气的15-40％。
4.权利要求1的方法，其中所冷凝的进料空气的第一部分占冷凝进料空气的25-75％；所冷凝的进料空气的第二部分占冷凝进料空气的25-75％。
5.权利要求1的方法，还包含将富氧液体从高压塔中导出、低温冷却所导出的富氧液体，将低温冷却的富氧液体分成第一部分和第二部分，将低温冷却的富氧液体的第一部分送入低压塔，蒸发低温冷却的富氧液体的第二部分以制得富氧蒸汽；将富氧蒸汽在低温冷却的富氧液体的第一部分被送入低压塔的位置下方1-10个平衡段处送入低压塔。
6.通过低温精馏进料空气生产高压氮和高压氧的设备，包括：
(A)包含第一塔、第二塔以及产品锅炉换热器的低温精馏设备；
(B)将进料空气送入产品锅炉换热器的装置，将进料空气从产品锅炉换热器送入第一塔的装置，以及将占总进料空气5-17.5％的进料空气从产品锅炉换热器中送入第二塔的装置；
(C)将至少占总进料空气20％的、来自第一塔上部的流体作为高压氮回收的装置；
(D)一台液体泵，将液体从第二塔下部送往液体泵的装置，以及将液体从液体泵送往产品锅炉换热器的装置；和
(E)将来自产品锅炉换热器的液体作为高压氧回收的装置。
7.权利要求6的设备，还包括汽轮骤冷器、将进料空气送往汽轮骤冷器的装置，以及将进料空气从汽轮骤冷器送入第二塔的装置。
8.权利要求6的设备，还包括汽轮骤冷器、将进料空气送往汽轮骤冷器的装置，以及将进料空气从汽轮骤冷器送入第一塔的装置。
9.权利要求6的设备，还包括过热器以及具有塔顶冷凝器的氩气塔，将流体从第一塔的下部送往过热器的装置，将所述液体的第一部分从过热器送入第二塔的装置，将所述流体的第二部分从过热器送往塔顶冷凝器的装置，以及将所述第二部分从塔顶冷凝器在所述第一部分被送入第二塔的位置下方1-10个平衡段处送入第二塔的装置。
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EP0866292A1 (en) 1998-09-23
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US5765396A (en) 1998-06-16
ID21666A (id) 1999-07-08
CN1106561C (zh) 2003-04-23
CA2232405A1 (en) 1998-09-19
KR100339631B1 (ko) 2002-07-18
CA2232405C (en) 2002-01-22

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