CN101479550B - 低温空气分离系统 - Google Patents

低温空气分离系统 Download PDF

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CN101479550B
CN101479550B CN2007800086886A CN200780008688A CN101479550B CN 101479550 B CN101479550 B CN 101479550B CN 2007800086886 A CN2007800086886 A CN 2007800086886A CN 200780008688 A CN200780008688 A CN 200780008688A CN 101479550 B CN101479550 B CN 101479550B
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N·M·普罗塞尔
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Praxair Technology Inc
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Abstract

本发明涉及一种通过低温精馏分离空气的系统，其中用两个单独的涡轮膨胀机(14，24)增加液体产量，一个(14)在不高于足以对低压塔(42)送料的压力排放，另一个(24)在不低于足以对高压塔(40)送料的压力排放，并且其中一个涡轮膨胀机(24)用环境温度或适度冷却的进料空气进料，且优选根据是否需要较大量或较小量液体产物间歇操作。

Description

低温空气分离系统
技术领域
本发明整体涉及低温空气分离，更具体地讲，涉及提高液体产物量的低温空气分离。
背景技术
低温空气分离是一种能源密集过程，因为需要低温致冷驱动该过程。在回收大量液体产物致使必然从系统移除大量致冷时尤其如此。因此，非常需要一种操作低温空气分离设备的方法，所述设备能够以低液体产生模式和高液体产生模式有效操作。
发明概述
一种利用具有高压塔和低压塔的双塔操作低温空气分离设备的方法，所述方法包括：
(A)将具有125K至200K温度的第一气流通到冷涡轮机，使第一气流在冷涡轮机中涡轮膨胀到高于低压塔操作压力不大于3psi的压力，并使涡轮膨胀的第一气流通入低压塔、大气和产物流中至少之一；和
(B)将具有200K至320K温度的第二气流通到热涡轮机，使第二气流在热涡轮机中涡轮膨胀到不低于高压塔操作压力的压力，并使涡轮膨胀的第二气流通入高压塔和冷涡轮机中至少之一。
本文所用术语“塔”是指蒸馏或分馏塔或区域，即接触塔或区域，其中液相和气相逆向接触实现流体混合物的分离，例如，气相和液相在塔内安装的一系列垂直隔开的盘或板上接触，和/或在填充元件(如结构或无规填充元件)上接触。关于蒸馏塔的其他细节，见Chemical Engineer′s Handbook，第5版，R.H.Perry和C.H.Chilton编著，McGraw-Hill Book Company，New York，Section13，TheContinuous Distillation Process。双塔包括高压塔，所述高压塔具有与低压塔下端有热交换关系的上端。
蒸气和液体接触分离过程取决于组分的蒸气压差。较高蒸气压(或者更易挥发或低沸点)的组分倾向于在气相中浓集，而较低蒸气压(或者不易挥发或高沸点)的组分倾向于在液相中浓集。部分冷凝是可用蒸气混合物冷却使挥发性组分在气相中浓集，因此不易挥发组分在液相中浓集的分离过程。精馏或连续蒸馏是组合由气相和液相逆向处理得到的连续部分蒸发和冷凝的分离过程。气相和液相逆向接触一般绝热，并可包括相间的积分(逐级)或微分(连续)接触。利用精馏原理分离混合物的分离工艺装置通常互换称为精馏塔、蒸馏塔或分馏塔。低温精馏为至少部分在或低于150开氏温度(K)进行的精馏过程。
本文所用术语“间接热交换”是指两种流体达到热交换关系而没有流体彼此之间的物理接触或互混。
本文所用术语“进料空气”是指主要包含氧、氮和氩的混合物，如环境空气。
本文所用术语塔的“上部”和“下部”是指相应在塔中点之上和之下的那些塔的部分。
本文所用术语“涡轮膨胀”和“涡轮膨胀机”或“涡轮机”分别指高压流体流动通过涡轮机装置以降低流体的压力和温度，从而产生致冷的方法和装置。
本文所用术语“低温空气分离设备”是指其中进料空气由低温精馏分离以产生氮、氧和/或氩的塔以及互连管、阀、热交换器等。
本文所用术语“压缩机”是指通过做功增加气体压力的机器。
本文所用术语“过冷”是指将液体冷却到低于现有压力液体饱和温度的温度。
本文所用术语塔的“操作压力”是指在塔底部的压力。
附图简述
图1-5为实施本发明低温空气分离方法的优选布置的示意图。
图6为在图1所示本发明低温空气分离系统实施中主热交换器冷却曲线的图解表示。
在附图中共同元件的数字符号是相同的。
发明详述
一般来讲，本发明为一种操作低温空气分离设备的方法，其中气流可以为进料空气或来自高压塔的富氮蒸气，并且具有通常在125K至200K，更优选140K至190K的温度，通过第一涡轮机(也称为冷涡轮机)涡轮膨胀到高于低压塔操作压力不大于3磅/平方英寸(psi)的压力。出自冷涡轮机的出料通入低压塔和/或排到大气或回收为产物。在冷涡轮机操作的至少一段时间，具有一般在200K至320K，更优选280K至320K温度的进料空气流，通过第二涡轮机(也称为热涡轮机)涡轮膨胀到不低于高压塔操作压力的压力。出自热涡轮机的出料通入高压塔和/或冷涡轮机。通过终止加压空气流到热涡轮机和增压机或关闭其进料压缩机，可关闭热涡轮机，以便在需要产生较少液体产物时降低功率消耗。此外，根据是否需要较大量或较小量液体产物产量，可将热涡轮机和增压机的供应流和/或入口压力调节到正常操作范围内。
以下参考附图更详细描述本发明。附图所示的低温空气分离设备包括具有高压塔40和低压塔42的双塔与氩塔44。冷涡轮机标为数字14，热涡轮机标为数字24。
现在参考图1，进料空气60在压缩机1中压缩，压缩的进料空气流61在后冷却器3中冷却，以产生流62。在压缩到对高压塔供料的足够压力且在后冷却后，将空气流62通到预纯化器5。流63分为流64、70和80。流64代表流63的最大部分。此流直接送到主热交换器50，在此冷却到略高于其露点温度，并作为流66送到高压塔40的底部。空气增压压缩机7压缩空气流70，产生压缩流71和90。压缩机7的排出压力(流71压力)与进入热交换器50的泵输液氧(流144)的压力相关。流71的流量一般为总空气流量的26％-35％。在通过后冷却器8后，流72在热交换器50中冷却和冷凝(或者假冷凝，如果高于超临界压力)。使流74在液体涡轮机30中压力降低到对高压塔40供料的足够压力。如图2所示，在较低氧沸腾压力液体涡轮机30由节流阀31代替。将流75分开，液体空气流的一部分76引入高压塔40，高于底部数级，其余部分77通过节流阀170减压，并作为流78引入低压塔。
流90显示从压缩机7的级间抽取，优选在压缩的第一级或第二级之后抽取。流90的压力可以为130磅/平方英寸绝对压力(psia)至400psia。流90在中间冷却器(未显示)后抽取，因此冷却到接近环境温度。如果泵输的液氧压力低，则压缩机7的排出压力对流90而言可能令人满意地高。在此情况下，流90在通过后冷却器8后，作为分流从流72抽取，如图2所示。图2显示具有相对较低泵输氧压的图1布置的变化。其中用节流阀31代替液体涡轮机。
驱动增压机20的热涡轮机24是本发明的重要组成部分。流90在增压压缩机20中压力升高，增压压缩机20由涡轮机24通过轴25提取的工作能驱动。流91的压力可以为220psia至900psia。在冷却器22中冷却到接近环境温度后，流92在涡轮机24中减压。流94在不低于高压塔操作压力的压力排出，高压塔操作压力一般在60至100psia的范围内。流94温度可低至约155K，可高至约240K。主热交换器50优选被设计成具有最佳温度水平的侧集管(side header)。流94在进入热交换器50的侧集管时与供给高压塔的主进料流组合。对于特定流90压力，热涡轮机的自增压布置(20，24，25)极大增加跨涡轮机的压力比。如此使通过涡轮机24的所需流量达到最小限度。这很重要，因为通过涡轮机24的流量从热交换器50的热端转移。通过涡轮机24的流量越高，在热交换器50中的热端温差越大。这代表致冷损失的增加。对20和24所示的涡轮机/增压机布置是优选的，因为其给予接近理想的无量纲参数，产生有效气动设计而无需齿轮传动。然而，假使这成立的话，可将供选的涡轮机/增压机配置用于20和24，或者用发生器(generator)作为涡轮机负荷装置，而不是用增压机20。
图1所示实施方案中的冷涡轮机使进料空气膨胀到低压塔。优选使热涡轮机/增压机与涡轮机膨胀到低压塔或对不产生液体有效的一些其他涡轮机布置(如富氮蒸气从高压塔膨胀)组合。所示自增压的涡轮机结构通常是优选的。在此，流80在压缩机10中压力升高，压缩机10由冷涡轮机14通过轴15驱动。这也增加跨涡轮机14的压力比，降低所需流量，并给予较佳氩和氧的回收。所得流81通过冷却器12，所得流82在热交换器50中冷却到中间温度。流84的温度一般可低至125K，可高至200K，优选在140K至190K的范围内。在排到高于低压塔操作压力不大于3psi的压力，将流86送到低压塔42的适合阶段。在同样保持通过此单元较低流量的供选布置中，流80在压缩机70的第一级后抽取(可能与流90组合)，直接送到热交换器50，部分冷却并送到涡轮机14。在此，冷涡轮机载有发生器，并且由于在压缩机70的第一级中压缩流80，其压力比仍然很高。
在高压塔40内，进料空气由低温精馏分离成富氮蒸气和富氧液体。富氮蒸气从高压塔40的上部作为流200抽取，并且通过与主冷凝器36中的低压塔42底部液体间接热交换冷凝。所得冷凝的富氮液体202的一部分201作为回流返回到高压塔40。所得冷凝的富氮液体的另一部分110在热交换器48中过冷。所得的过冷富氮液体112通过阀172，并且作为流114进入低压塔112的上部。如果需要，可将流62的一部分116回收为液氮产物。
富氧液体从高压塔40的下部在流100中抽取，并在热交换器48中过冷以产生流102，通过阀171，然后作为流104通入低压塔42。在所示的实施方案中，低温空气分离设备也包括产生氩。在这些实施方案中，富氧液体102的一部分106通过阀173，作为流108通入氩塔顶冷凝器38处理，这将在以下进一步讨论。
低压塔42一般在16至26psia范围的压力操作。在低压塔42内，各种进料由低温精馏分离成富氮蒸气和富氧液体。富氮蒸气从低压塔42的上部在流160抽取，通过热交换器48和主热交换器50温热，并且作为气态氮产物在流163回收。为了控制产物纯度，废氮流150从塔42低于流160抽取水平抽取，并且在通过热交换器48和主热交换器50后从工艺在流153中移除。富氧液体从低压塔42的下部在流140中抽取，并且由低温液泵34泵升到较高压力，以形成加压的液氧流144。如果需要，可将流144的一部分142回收为液氧产物。其余部分通过主热交换器50由与进入的进料空气间接热交换气化，并在流145中回收为气态氧产物。
主要包含氧和氩的流从塔42在流120中通入氩塔44，在此分离成富氩顶部蒸气和较富氧的底部液体，底部液体在流121中返回到塔42。富氩顶部蒸气作为流122通入氩塔顶冷凝器38，在其中相对于在流108中提供到顶部冷凝器38的部分气化富氧液体冷凝。所得冷凝的氩123在流203中作为回流返回到塔44，并且流123的一部分126作为液氩产物回收。从顶部冷凝器38的所得富氧流体在蒸气流132和液体流130中通入低压塔42。
图6所示的热交换器50的冷却曲线证明增加热涡轮机24使液体产量更高。在冷却曲线的循环部分中可以看到，温热和冷却温度分布窄缩，然后在较热温度水平开始开放。这是由热涡轮机提供的致冷的结果。在此最小窄缩温度相当于热涡轮机排出流94对热交换器50供料的点。没有热涡轮机致冷，温热和冷却流的温度分布就会在热交换器的较高温度下交叉而不是开放。这意味不极大增加冷涡轮机14流就不能产生相同量的液体。冷涡轮机流增加会使氩和氧的回收很差。此外还需要用第二冷涡轮机(并联)处理大范围流量。有热涡轮机作为第二涡轮机，从而在最需要的热温度水平提供致冷更加有效。如果能够有效进行，在温热温度致冷很有效，在此通常就是这样。
图3实施方案是改型例子的最优选结构。它与图1的区别在于，在进料到热增压机和涡轮机(20和24)之前单独的压缩机(18)提高流90的压力。如果原始设计没有级间取出流，就不可能经济地改进压缩机7以处理对于改型从所需级间位置抽取流90。因此，最佳选择是用其他压缩机18将空气压力提高到热涡轮机/增压机所需的水平。根据跨热涡轮机的所需压力比，压缩机18优选为一级或两级。在加到增压机20前，冷却器19从流89移除压缩热量。
图4类似于图1，不同之处在于流93(涡轮机24的进料)通过在热交换器50中部分冷却而冷却到低于环境温度一定量。这只在有效产生比正常由图1实施方案产生的更高量的液体时是必须的。在此情况下，图1中的冷涡轮机流(涡轮机14)难以控制地变大。这表明在这些较高液体速率，需要在比环境温度水平进料操作涡轮机24所提供的更低温度水平致冷。通过部分使流93冷却，同样可在比冷涡轮机更高的温度水平有效(和更有效)提供其他涡轮机致冷，同时能够在足够低温度进一步增加液体产量。这还将降低热交换器50的热端温差，减少用环境水平涡轮膨胀产生的致冷损失。也可能需要此实施方案经济地使用低氧沸腾压力或在无氧沸腾的循环中使用的热涡轮机。
图5所示实施方案的关键特征是，排出流94与来自热交换器50的中间流组合为增压的冷涡轮机14供料。涡轮机24现在与涡轮机14串联。通常，这意味流94的压力较高，也意味流91、92和90的压力比图1实施方案更高。这就是为什么流90显示在冷却器8后作为分流从压缩机7的排放物抽取。然而这取决于压缩机7的排放压力，并且从压缩机7的级间位置抽取流90仍然可能合乎需要。在流94进料到热交换器50中的中间位置不实际时可使用此结构。一个实例是没有预设计侧喷嘴和分配器以接受热涡轮机排出流的热交换器50的设备改型。此结构通常导致多余流量通过涡轮机14。
虽然已关于某些优选的实施方案详细描述了本发明，但本领域的技术人员应认识到在权利要求精神和范围内有其他实施方案。

Claims (7)

1.一种利用具有高压塔和低压塔的双塔操作低温空气分离设备以精馏进料空气来制备液体产物的方法，所述方法包括：
压缩由进料空气组成的主进料空气流以制备压缩的主进料空气流，在主热交换器中冷却一部分压缩的主进料空气流并将所述压缩的主进料空气流引入高压塔；
将由另一部分主进料空气流组成的第一气流进一步压缩，在主热交换器中部分冷却第一气流，至少将具有125K至200K第一温度的第一气流通到冷涡轮机，使第一气流在冷涡轮机中涡轮膨胀到比低压塔操作压力高出不超过3psi的压力以制备涡轮膨胀的气流，并使涡轮膨胀的气流通入低压塔；
将由另一部分压缩的主进料空气流组成的第二气流进一步压缩，在增压压缩机中将第二气流至少部分进一步压缩，并且未在主热交换器中冷却，在通过增压压缩机后从第二空气流除去压缩热，然后将具有200K至320K第二温度的第二空气流通到驱动增压压缩机的热涡轮机，使第二气流在热涡轮机中涡轮膨胀到不低于高压塔操作压力的压力，并使涡轮膨胀的第二气流与第一气流一起通入冷涡轮机；或者使涡轮膨胀的第二气流与第一气流进入主热交换器的中间位置以及随后高压塔中；和
调节第二气流的流量或跨热涡轮机的压力比来改变液体产物的产量。
2.权利要求1的方法，其中至少一些氧产物作为液体产物从低温空气分离设备回收。
3.权利要求1的方法，其中至少一些氮产物作为液体产物从低温空气分离设备回收。
4.权利要求1的方法，所述方法进一步包括氩塔，使自低压塔的流体通到氩塔，并且从氩塔回收氩产物。
5.权利要求4的方法，其中至少一些回收的氩产物作为液体产物回收。
6.权利要求1的方法，其中所述第二温度为280K至320K。
7.权利要求1的方法，其中所述热涡轮机的操作是在冷涡轮机操作期间打开和关闭以调节进入热涡轮机的流量。
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KR20080100362A (ko) 2008-11-17
EP2010846B2 (en) 2014-11-19
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CN101479550A (zh) 2009-07-08
CA2645047A1 (en) 2008-05-08
CA2645047C (en) 2011-05-17
KR101275364B1 (ko) 2013-06-17
ES2360744T5 (es) 2015-03-05
ES2360744T3 (es) 2011-06-08
WO2008054469A2 (en) 2008-05-08
US7533540B2 (en) 2009-05-19
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BRPI0707994A2 (pt) 2011-05-17

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