CN1098448C - 用于生产低纯氧和高纯氧的低温精馏系统 - Google Patents

用于生产低纯氧和高纯氧的低温精馏系统 Download PDF

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CN1098448C
CN1098448C CN97117345A CN97117345A CN1098448C CN 1098448 C CN1098448 C CN 1098448C CN 97117345 A CN97117345 A CN 97117345A CN 97117345 A CN97117345 A CN 97117345A CN 1098448 C CN1098448 C CN 1098448C
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tower
purity oxygen
oxygen
argon
rich
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CN1184925A (zh
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D·P·波拿奎斯特
N·J·莱恩希
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Praxair Technology Inc
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Abstract

使用具有底部再沸器的旁塔、具有高的高纯氧和低纯氧回收率的低温精馏系统，在其中进料空气被部分冷凝，部分冷凝后在进行精馏前，残留的进料空气蒸汽被汽轮膨胀。

Description

用于生产低纯氧和高纯氧的低温精馏系统
本发明总的涉及进料空气的低温精馏，更具体地说涉及进料空气的低温精馏以生产低纯氧和高纯氧。
在诸如玻璃制造、炼钢和能量生产的应用中对低纯氧的需求不断增加。一般通过进料空气在一双塔中的低温精馏来大量生产低纯氧，在双塔中处于高压塔压力的进料空气被用来再沸低压塔液本底部残留物，然后被送入高压塔内。
一些低纯氧的用户如大型钢铁厂除了低纯气态氧外，还常常需求一些高纯氧。虽然常规系统已可能生产一些与低纯氧一起的高纯氧，但它还不能生产大量的与低纯氧一起的高纯氧。
因此本发明的目的之一是提供一种以高回收率有效生产低纯氧和高纯氧的低温精馏系统。
由于有时候需要回收与低纯氧和高纯氧一起的氢，因此本发明的目的之二是提供除了低纯氧和高纯氧之外还能生产氢的低温精馏系统。
此外，有时还需要生产与低纯氧和高纯氧一起的液态氮，因此本发明的目的之三是提供一除了低纯氧和高纯氧外还可生产液态氮的低温精馏系统。
通过本发明实现了上述和其它目的，本领域技术人员在阅读了本公开后将变得显而易见。本发明的一方面是：
生产低纯氧和高纯氧的方法，它包括：
(A)通过与高纯氧进行间接热交换而部分冷凝进料空气以生产液态进料空气和气态进料空气；
(B)汽轮膨胀所述气态进料空气并将已汽轮膨胀的气态进料空气送入中压塔内；
(C)在中压塔内通过低温精馏系分离进料空气以生产富氮流体和富氧流体，并将富氮流体和富氧流体送入低压塔内；
(D)通过低温精馏在低压塔内制得富氮流体和富氧流体，并将富氧流体从低压塔送入一旁塔中；和
(E)在所述旁塔内通过低温精馏，将富氧流体分离成低纯氧和高纯氧，从旁塔中回收低纯氧并从旁塔中回收高纯氧。
本发明的另一方面是：
制备低纯氧和高纯氧的设备，它包括：
(A)第一塔、第二塔以及具有再沸器的旁塔；
(B)汽轮骤冷器、用于将进料空气送入旁塔再沸器的装置以及用于将进料空气从旁塔再沸器送入汽轮骤冷器的装置；
(C)用于将进料空气从汽轮骤冷器送入第一塔的装置，以及用于将来自第一塔的流体送入第二塔的装置；
(D)用于将流体从第二塔送入旁塔的装置；和
(E)用于从旁塔回收高纯氧的装置，以及用于从旁塔中高纯氧从旁塔回收的位置上方回收低纯氧的装置。
此处所用的术语“进料空气”意指主要包含氧、氮和氢的混合物如环境空气。
此处所用的术语“塔”意指一蒸馏或分馏塔或区，即一接触塔或接触区，其中液相和气相逆流接触以有效地分离流体混合物，如通过气相和液相在装于塔内的一系列垂直放置的塔盘或塔板上和/或在填料单元如结构或无规填料上接触。对于蒸馏塔的进一步讨论，可参见《化学工程师手册》，第5版，R.H.Perry和C.H.Chilton编，McGraw-Hill Book Company出版，纽约，第13章，“连续蒸馏法”。
气-液接触分离法取决于各组分蒸气压的不同。高蒸气压(或易挥发或低沸点)组分将易于浓集于气相中，而低蒸气压(或难挥发或高沸点)组分将易于浓集于液相中。部分冷凝是藉可用蒸气混合物的冷却以浓集气相中的挥发组分，因而是在液相中挥发组分较少的分离方法。精馏或连续蒸馏是结合通过气液相的逆流处理获得的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，并可包括相之间的积分(分段的)或微分(连续的)接触。利用精馏的原理来分离混合物的分离方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为150K或低于150K下进行的精馏方法。
此处所用的术语“间接热交换”意指在流体相互之间没有任何物理接触或混合的条件下将两种流体导入热交换关系。
此处所用的术语“再沸器”意指从塔中液体产生塔上流蒸气的热交换装置。再沸器可位于塔内或塔外。底部再沸器是从塔的底部即从传质单元下方使液体蒸发的再沸器。
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一透平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”意指分别位于塔中点以上和以下的塔的部分。
此处所用的术语“塔盘”意指一接触段(它不必是一平衡段)，也意指其它接触设备如分离能力相当于一个塔盘的填料。
此处所用的术语“平衡段”意指气-液接触段，在其中离开该段的蒸气和液体处于传质平衡，如具有100％效率的塔盘或相当于一理论塔板(HETP)的填料单元高度。
此处所用的术语“低纯氧”意指氧浓度在50-98％(摩尔)范围内的流体。
此处所用的术语“高纯氧”意指氧浓度大于98％(摩尔)的流体。
此处所用的术语“氩塔”意指处理含氩进料并生产出氩浓度超过进料中氩浓度的产品的塔。
图1是本发明一个优选实施方案的示意图。
图2是本发明另一个优选实施方案的示意图，其中也可生产液体氮。
图3是本发明还一个优选实施方案的示意图，其中也可生产氩。
本发明将参照附图进行详细描述。现参照图1，已清除高沸点杂质如水蒸气、二氧化碳和碳氢化合物并被压缩至一般为0.3447-0.4137MPa[50-60psia(磅/平方英寸(绝对压))]的进料空气60与经过主换热器1的回流进行间接热交换而被冷却。所得冷却进料空气流61被送入旁塔11的底部再沸器20，在其中通过与包含高纯氧的旁塔11底部液体进行间接热交换而被部分冷凝。在底部再沸器20中，所述进料空气的部分冷凝产生了液态进料空气和剩余的气态进料空气，这些液态进料空气和剩余的气态进料空气以两相流62被送进相分离器40。
由塔底再沸器20中进料空气的部分冷凝所得的气态进料空气被汽轮膨胀然后送入第一或中压塔10的下部。示于图1的本发明实施方案是一优选实施方案，在其中该气态进料空气在汽轮膨胀前至少部分被过热。现参照图1，在底部再沸器20中间进料空气的部分冷凝所得的气态进料空气从相分离器40以流63出来。流63的第一部分64通过部分横过主换热器1被加热以形成加热流65。流63的第二部分66被送经阀67，所得流68与流65汇合形成流69，该流69通过流经汽轮骤冷器30被汽轮膨胀至大约中压塔10的操作压力以产生制冷作用。所得汽轮膨胀进料空气流70从汽轮骤冷器30中出来被送入中压塔10的下部。已清除高沸点杂质并压缩至压力为0.8274-3.447MPa[120-500psia]的第二进料空气流80通过主换热器1被冷却，所得冷却进料空气流81也被送入中压塔10中。
中压塔10在压力一般为0.2068-0.2758MPa[30-40psia]的范围内并低于双塔系统中常规高压的操作压力下操作。在中压塔10中通过低温精馏将进料空气分离成富氮蒸气和富氧液体。富氮蒸气从中压塔10的上部出来以流92进入低压塔12的底部再沸器21，在其中通过与低压塔21底部流体进行间接热交换而得到冷凝。所得富氮流93被分离成作为回流进入塔10上部的第一部分94以及通过过冷器或热交换器2而得到低温冷却的第二部分95。低温冷却流96流经阀97然后以流98作为回流被送入低压塔12的上部。
在底部再沸器20中的进料空气的部分冷凝产生的液体进料空气被送入低压塔12中。富氧液体从中压塔10的下部被送入低压塔12中。示于图1的本发明实施方案是一优选实施方案，其中这两种液体汇合在一起并被送入低压塔中。参照图1，在底部再沸器20内由进料空气的部分冷凝所得的液体进料空气作为流71从相分离器40中导出并流经阀72。富氧液体以流73从中压塔10的下部导出，与流71汇合形成流74。流74通过流经过冷器3而被低温冷却，所得流75流经阀76然后作为流77进入低压塔12中。已清除高沸点杂质并被压缩至压力为0.3447-0.4137MPa[50-60psia]的第三进料空气流82通过流经主换热器1而被冷却。所得流83通过流经换热器4而进一步得到冷却。所得流84流经阀85，然后作为流86进入低压塔12的上部。
第二塔或低压塔12在低于中压塔10的压力一般在0.1241-0.1517MPa[18-22psia]的范围内下操作。在低压塔12内各种进入该塔的进料通过低温精馏被分离成富氮流体和富氧流体。富氮流体作为流100从低压塔12的上部导出，通过流经热交换器2、3、4和1而得到加热，并以流102从系统中除去，流102可作为氮浓度等于或大于99％(摩尔)的产品氮气全部或部分回收。富氧流体以液流91从低压塔12的下部导出，并被送入旁塔11的上部。
旁塔11在压力一般为0.1241-0.1517MPa[18-22psia]下操作。在旁塔11内通过低温精馏将富氧流体分离成低纯氧和高纯氧。顶部蒸气流90从旁塔11的上部被送入低压塔12的下部。
低纯氧和高纯氧中的一个或两个可作为用于回收的液体或蒸气从旁塔11中导出。高纯氧以液体的形式聚集在旁塔11的底部，一些这种液体被蒸发以进行上述底部再沸器20中进料空气的部分冷凝。在示于图1的本发明的实施方案中，高纯氧以液体形式从旁塔11流106中被导出，且流106的一部分107作为产品流体高纯氧回收。流106的另一部分108经液体泵34被泵至较高压力，所得加压流109通过主换热器1得到蒸发并以流110作为加压高纯氧得到回收。
低纯氧在高纯氧从旁塔11中导出的位置上方15-25个平衡段的位置从旁塔11中导出。在示于图1的本发明实施方案中，低纯氧作为液体以流103从旁塔11中导出，并通过液体泵35泵至较高压力。加压流104经至换热器1得到蒸发并以流105作为产品加压低纯氧回收。
通过本发明的实施，除了能回收低纯氧外，还可回收大量的纯氧。一般而言通过本发明的实施，以气态和/或液体形式回收的高纯氧的量将是以气态和/或液体形式回收的低纯氧的量的0.5-1.0倍。
通过从塔11的底部上方的位置导出低纯氧将能产生大量的高纯氧。和塔内从置于其底部的再沸器20上升的蒸气量(V)相比，该氧的导出减少了沿那个位置下行的液体量(L)。对于自塔11底部取出的液体氧流106所能达到的纯度受限于塔11内流103被导出的位置下方的L/V比，该比值越大，则流106越不纯。凭借流103的导出，由于L/V比值的减少，从塔11底部的高纯氧的生产因此而变得便利。此外，通过去除作为进料空气组分之一的进入该处理的氩也能生产出高纯氧。氩易聚集在塔11内下行液体中。正常情况下氩在液体的聚集使高纯氧的生产变得困难。但由于流103含有在进料空气中大部分的进入所述设备的氩，在塔中流103导出位置的下方氩的聚集被降低。
图2说明本发明的另一实施方案，其中也可生产液氮及大量的液体高纯氧。图2中的普通单元的标号相应于图1中的那些普通单元的标号，这些普通单元将不再详细讨论。
现参照图2，已清除高沸点杂质的所有进料空气被压缩至一般在0.5516-6.895MPa[80-1000psia]范围内的高压。进料空气流45被送入主换热器1内并且在部分横过主换热器1后，一部分120被导出。剩余部分46完全通过主换热器1，并被分成如前述示于图1中实施方案般处理的流82和83。部分120被送至汽轮骤冷器32，在其中被汽轮膨胀至类似于示于图1实施方案的进料空气流60的压力。已汽轮膨胀的流121从汽轮骤冷器导出，返回到主换热器1内，从中以如前述般处理的流61的形式出现。富氮液流96的一部分112流经阀113并作为氮浓度等于或大于99％(摩尔)的液氮产品的回收。
图3说明了本发明的又一实施方案，其中附加生产氩产品。图3中对于普通单元的数字相应于图1中的数字，并将不再详细讨论。
现参照图3，主要包含氧和氩的流117从旁塔11中低纯氧流体以流103从旁塔导出的位置下方处导出。氩塔进料流117被送入氩塔13，在其中流117被低温冷却，分成富氩流体和富氧流体。富氧流体以流116从氩塔13下部导出被送回旁塔11中。富氩流体作为氩浓度一般为95-100％(摩尔)的产品氩从氩塔13的上部回收。在示于图3的本发明实施方案中，产品氩作为液体形式回收。再参照图3，富氩蒸气以流112从氩塔13的上部导出，并进入冷凝器或再沸器22而在其中得到冷凝。所得冷凝富氩液体以流113从冷凝器22中导出并被分成作为回流进入氩塔13的第一部分114和作为产品氩回收的第二部分115。冷凝器22通过来自低压塔12的流体来驱动。液流110从低压塔12再沸器21上方4-10个平衡段的位置导出，并送入冷凝器22，其中通过与正在冷凝的富氩蒸气进行间接热交换器而被蒸发。所得蒸气以流111返回低压塔12中。在冷凝器22中进行的热交换可互换地在低压塔12内置于大约在流11被导出的位置处的再沸器中进行。富氩蒸气可互换地通过与中压塔出来的富氧流体进行间接热交换而得到冷凝。
虽然本发明已参照特定实施方案做了详述，但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还有本发明的其它实施方案。

Claims (10)

1.生产低纯氧和高纯氧的方法，包括：
(A)通过与高纯氧进行间接热交换而部分冷凝进料空气以生产液态进料空气和气态进料空气；
(B)汽轮膨胀所述气态进料空气并将已汽轮膨胀的气态进料空气送入中压塔内；
(C)在中压塔内通过低温精馏分离进料空气以生产富氮流体和富氧流体，并将富氮流体和富氧流体送入低压塔内；
(D)通过低温精馏在低压塔内制得富氮流体和富氧流体，并将富氧流体从低压塔送入一旁塔中；和
(E)在所述旁塔内通过低温精馏，将富氧流体分离成低纯氧和高纯氧，从旁塔中回收低纯氧并从旁塔中回收高纯氧。
2.如权利要求1的方法，其中在所述部分冷凝前将进料空气汽轮膨胀。
3.如权利要求2的方法，其中将步骤(C)中所述的富氮流体的一部分作为产品氮回收。
4.如权利要求1的方法，还包括将含氩流体从旁塔送入氩塔，在氩塔内通过低温精馏生产富氩流体，并从氩塔回收富氩流体作为产品氩。
5.如权利要求4的方法，其中通过与来自低压塔和中压塔中至少一个塔的流体进行间接热交换而将来自氩塔上部的蒸气冷凝。
6.如权利要求1的方法，还包括将液体进料空气送入低压塔中，所述液体进料空气是通过与高纯氧进行间接热交换而部分冷凝进料空气而产生的。
7.生产低纯氧和高纯氧的设备，包括：
(A)第一塔、第二塔以及具有再沸器的旁塔；
(B)汽轮骤冷器、用于将进料空气送入旁塔再沸器的装置以及用于将进料空气从旁塔再沸器送入汽轮骤冷器的装置；
(C)用于将进料空气从汽轮骤冷器送入第一塔的装置，以及用于将包括富氮流体和富氧流体的流体从第一塔送入第二塔的装置；
(D)用于将所述富氧流体从第二塔送入旁塔的装置，在所述旁塔内所述富氧流体被分离成低纯氧和高纯氧；和
(E)用于从旁塔回收所述高纯氧的装置，以及用于从旁塔中所述高纯氧从旁塔回收的位置上方回收所述低纯氧的装置。
8.如权利要求7的设备，其中用于将进料空气送入旁塔再沸器的装置包括汽轮骤冷器。
9.如权利要求7的设备，还包括一氩塔、用于将含氩流体从旁塔送入该氩塔的装置以及用于从该氩塔的上部回收氩产品的装置。
10.如权利要求9的设备，还包括与氩塔上部以及与第二塔处于流体连通的热交换器，所述第二塔与所述热交换器连通的位置在第二塔底部上方4-10个平衡段。
CN97117345A 1996-12-12 1997-08-08 用于生产低纯氧和高纯氧的低温精馏系统 Expired - Fee Related CN1098448C (zh)

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