CN103270381B - 一种用于使气体液化的系统和工艺 - Google Patents

一种用于使气体液化的系统和工艺 Download PDF

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CN103270381B
CN103270381B CN201080068287.1A CN201080068287A CN103270381B CN 103270381 B CN103270381 B CN 103270381B CN 201080068287 A CN201080068287 A CN 201080068287A CN 103270381 B CN103270381 B CN 103270381B
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pressure
storage container
phase
high pressure
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CN103270381A (zh
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P.希金博萨姆
A.K.J.托法姆
K.D.T.塔普斯菲尔德
J.C.罗斯曼
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Air Products and Chemicals Inc
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
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    • F25J2270/00—Refrigeration techniques used
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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Abstract

一种用于使气体液化的系统和工艺，其包括：将供应流引入到至少包括温膨胀器和冷膨胀器的液化器内；将供应流在液化器内压缩到大于它的临界压力的压力并且将压缩供应流冷却到低于它的临界温度的温度以形成高压密相流；从液化器移除高压密相流，在膨胀装置中减小高压密相流的压力，以形成所得两相流并且然后将所得两相流直接地引入到存储容器内；并且将所得两相流的闪蒸部分与来自存储容器中的液体的沸腾蒸气组合，以形成组合蒸气流，其中，高压密相流的温度低于冷膨胀器的排出流的温度。

Description

一种用于使气体液化的系统和工艺
背景技术
氮气液化器在本领域中为熟知的并且通常链接到氮气生成器，例如，或者空气分离单元(ASU)。例如，液化器可用来液化来自ASU的低压气态氮气。液化器还可在更高压力处和/或低温温度处获取来自ASU的它们的供应的至少一部分用于液化目的。
在传统液化工艺中，高压氮气被冷却到低温温度，以形成密相流体(即低于它的临界温度并且高于它的临界压力的流体)并且然后通常通过阀或密流体膨胀器的使用在压力方面减小，使得它主要形成具有某些闪蒸蒸气(flashvapor)的液体。该两相混合物然后被供应到分离器。冷膨胀器还典型地排出蒸气或轻微液化流到分离器内。例如，来自分离器的蒸气被重新加温到环境温度并且然后在工艺中再循环，同时液体在被供应到隔离液体存储容器之前过冷却。该过冷却可在更低压力处通过在第二分离器中的压力减小、或间接地在过冷却器中在低压处通过相对沸腾液体的换热而发生。例如，过冷却器的使用允许足够的压力被维持在液体中，以将它传递到存储器，而不使用泵。
例如，在液化器中产生的液体的部分可被存储例如在隔离液体存储容器中用于未来使用或者通过公路容器车输出，同时液体的其它部分可返回到ASU以提供制冷。
如果第二分离器被使用，则当额外的泵的使用被避免时第二分离器必须被提高在存储容器的水平之上。
在隔离液体存储容器中的液体的存储然而不是简单的办法。例如，热由于不完善的隔离而从环境最终泄漏到隔离液体存储容器中。另外，在隔离液体存储容器中存储的液体的部分蒸发并且要求额外液体的产生，以补偿这种损失。传统地，作为在隔离液体存储容器中蒸发的液体的结果形成的冷蒸气排放到大气，以避免隔离液体存储容器的压力升高，然而制冷然后在工艺中丧失了。
先前公开的链接到ASU设备的氮气液化器因此由于若干原因而为有问题的。第一，从隔离液体氮气容器回收闪蒸或冷沸腾蒸气要求冷送风机的使用。冷送风机用来为来自容器的闪蒸或冷沸腾蒸气增压，使得它处于足够的压力，以被送回到液化器或ASU，以允许它的制冷恢复。然而，制冷的仅仅部分当送风机被使用时可恢复，这是因为送风机的功率作为热最终增加到沸腾蒸气的冷流。另外，送风机对安装和维护为不方便的并且昂贵的，并且还增加这些系统和工艺的复杂性，因而使送风机的使用不经济。
第二，冷端液体氮气分离器的使用增加工艺的复杂性，并且使它成本更高地执行，这是因为它们必须被包围在隔离冷箱内。当安排运输路径时大以及复杂的冷箱难以处理，这是因为对于这种大的预隔离负载(即冷箱负载)某些目的地位置可难以或甚至不能达到。
第三，液化工艺典型地包括过冷却器，以减少在容器中形成的闪蒸气体。这种过冷却器还增加工艺的不期望的成本和复杂性。
另外，尽管早期液化器(即在现在传统地使用的液化器之前使用的液化器)采用单一膨胀器并且利用仅仅单一分离器装置，但是这些早期液化器相对效率低。为了增加液化器的效率，后期液化器设计使用多个膨胀器和多个分离器以在中压处回收闪蒸蒸气。在中压处闪蒸蒸气的回收对于这么多年到这些天，被认为是必须的，这是因为作为进入液体存储容器的液体产品的结果形成的闪蒸蒸气为不期望的并且因而将排放到大气，以控制存储容器的压力。这种排放将当然导致来自闪蒸蒸气的珍贵的制冷的丧失。
因而，在工业气体行业中需要简单并且低成本液化工艺，其具有容器闪蒸和沸腾蒸气回收的效率优点，而不具有冷送风机、冷端分离器或过冷却器的复杂性。
发明内容
描述的实施例通过提供简化和有效的液化器而满足本领域中的要求，该液化器使用液体存储容器作为闪蒸分离器并且通过液化器从存储器回收闪蒸和沸腾蒸气。分离器和过冷却器可从液化器设计和工艺中消除。因为液化器的冷部基本上为仅仅换热器和管道系统，所以它可被直接地隔离并且分离冷箱结构被消除。描述的实施例利用相反于传统知识的设计和工艺用于有效的液化器设计和工艺的构建。
在分离液化器中而不是在ASU设备中产生液体具有操作性优点，诸如易于根据需要打开和关闭，但是具有与分离工艺单元相关的高资本成本和更低的效率的显著缺点。总体上，增加工艺效率将增加资本成本，并且资本成本必须增加以改善效率。该描述的工艺和系统允许该资本成本减小同时改善效率。
在一个实施例中，公开用于使气体液化的工艺，其包括：将供应流引入到至少包括温膨胀器和冷膨胀器的液化器内；将供应流在液化器中压缩到大于它的临界压力的压力并且将压缩供应流冷却到低于它的临界温度的温度，以形成高压密相流；从液化器移除高压密相流并且在膨胀装置中减小高压密相流的压力，以形成所得两相流并且然后将所得两相流直接地引入到存储容器内；并且将所得两相流的闪蒸部分与来自存储容器中的液体的沸腾蒸气组合，以形成组合蒸气流，其中，高压密相流的温度低于冷膨胀器的排出流的温度。
在另一个实施例中，公开了用于使大气气体液化的系统，其包括：用于接收供应流的第一导管；液化器，其流体地连接到第一导管用于压缩并且冷却供应流，以形成高压密相流体，其中，液化器至少包括温膨胀器、冷膨胀器、用于将供应流压缩到大于它的临界压力的压力的压缩器、和用于将压缩供应流冷却到低于它的临界温度的温度的换热器；第二导管，其流体地连接到液化器用于从液化器接收高压密相流；第一膨胀装置，其流体地连接到第二导管，以减小高压密相流的压力，以形成所得两相流；第三导管，其流体地连接到第一膨胀装置用于接收两相膨胀流；和存储容器，其流体地连接到第三导管用于接收并且存储两相膨胀流，其中，存储容器设计成在处于或低于1.5巴(绝对压力)(bara)的压力处操作，并且其中，换热器设计成使得高压密相流的温度低于冷膨胀器的排出流的温度。
附图说明
前述总结以及示范性实施例的以下详细描述当结合附图阅读时更好理解。为了示出实施例的目的，在附图中示出示范性结构；然而，本发明不限于公开的特定方法和手段。在附图中：
图1为根据本发明的、用于将液体存储容器使用为闪蒸分离器以及通过液化器从存储器回收闪蒸和沸腾蒸气的示范性工艺的流程图；
图2为包括不同液化器构造的可选示范性工艺的流程图；
图3为具有与图1所示的相同膨胀器构造的先前公开的工艺的流程图，其中，该工艺包括冷端分离器和过冷却器，但是不包括从容器回收闪蒸蒸气或沸腾；和
图4为示出用于使图1的示范性工艺与空气分离单元相集成的各种方法的流程图，其中根据本发明的任何其它工艺可以以相似方式与空气分离单元相集成。
具体实施方式
图1示出用于将液体存储容器170使用为闪蒸分离器并且通过液化器101从液体存储容器170回收闪蒸和沸腾蒸气的示范性系统和工艺。图1公开低压氮气供应流100，其与加温容器闪蒸和沸腾蒸气流102组合，以形成组合流104。例如，低压供应流100可为氮气，或者它可为另外的气体或气体混合物，诸如空气、氧气、氩气、一氧化碳、氖气、乙烯、氦气、或氢气。组合流104然后在供应压缩器106中被压缩到大约6巴(绝对压力)，以形成压缩流108。压缩流108然后在后冷却器110中被冷却，以形成冷却流112。冷却流112然后与再循环流114组合，以形成流116。流116然后在再循环压缩器118中被压缩到大约32巴(绝对压力)，从而导致压缩流120。流120然后在后冷却器122中被冷却，以形成流124。流124然后分成流126和128。
流126(任选地)在换热器130中被冷却，以形成流132。流132然后在温膨胀器134中膨胀到大约6巴(绝对压力)，以形成温膨胀流136。
流128在温压伸器(compander)压缩器138中被进一步压缩，以形成流140。流140然后在温压伸器后冷却器142中被冷却，以形成冷却流144。冷却流144然后又在冷压伸器压缩器146中被压缩到大约65巴(绝对压力)，以形成压缩流148。压缩流148然后又在冷压伸器压缩器后冷却器150中被冷却，以形成高压流152。该高压流152在换热器130中被冷却到大约182K的中间温度，从而产生流154和156。
流156在冷膨胀器158中膨胀，以形成排出流160。排出流160返回到换热器130的冷端，其中它被加温并且与来自温膨胀器134的排气流136混合以形成流162。流162在换热器130中被加温，以形成再循环流114。再循环流114然后与压缩供应流112混合并且被供应到再循环压缩器118的抽吸部。
流154在换热器130中被进一步冷却，以形成高压密相流164。高压密相流164在大约96K的温度处从换热器130的冷端抽出，横跨一个或多个膨胀装置166在压力方面降低，以形成流168，其中流168被直接地供应到液体存储容器170内。如在此使用，术语“被直接地供应”应意指指定流在离开一个或多个膨胀装置166后经由导管被提供到液体存储容器170，而不遇到将改变指定流的成分、温度或压力的任何另外的器械。另外，如在此使用“被直接地连接”应意指器械的第一装置或第一件连接到器械的第二装置或第二件，而不具有将改变经过(例如第一装置到第二装置)的流的成分、温度、或压力的器械的任何中间装置或中间件。
流168被闪蒸到液体存储容器170内，以主要产生具有某些蒸气的液体。来自流168的液体将增加到已经在液体存储容器170中存在的液体，同时闪蒸蒸气将与在液体存储容器170中已经存在的沸腾蒸气组合。由闪蒸蒸气和沸腾蒸气组成的组合蒸气流172从液体存储容器170中抽出，并且在正常操作期间，被供应到液化器101的换热器130作为流174。流174在换热器130中加温以形成加温容器闪蒸和沸腾蒸气流102并且与低压供应100混合以形成组合流104，从而进入液化器101的构成压缩器106。
如果液化器101没有操作，则液体存储容器170沸腾蒸气可从液体存储容器170移除为组合蒸气流172、176，横跨一个或多个膨胀装置178在压力方面减小以形成流180，并且排放到大气中，以控制液体存储容器170的压力。
该系统布置的显著优点中的一个为简化的设计。换热器130、膨胀器134、158和相关的管道系统可例如利用隔离材料(诸如矿棉、聚氨酯泡沫体、泡沫玻璃、“制冷剂(cryogel)”或合适的替代物)分离地隔离，或者安装在由隔离的管道系统连接的小的本地冷箱中。当处理并且安排运送路线时减小冷箱的尺寸要求特别地重要，这是因为对于更大的预隔离负载(即冷箱负载)某些目的地位置可难以或不能达到
另外，相反于传统看法，相比于其中沸腾气体没有回收的先前设计，从液体存储容器170回收沸腾蒸气令人吃惊地改善液化器101和存储系统的整体效率达大约0.5-1.0%(根据液体存储容器170和液化器101的相对尺寸和容器隔离的质量)，这是因为它的冷用来部分地冷却产品并且减小液化器101所需要的功率，而不是通过将它直接地排放到大气而浪费。另外，需要的氮气供应流减小了(这是因为先前排放的氮气被回收)，这可导致更小的ASU的使用。
如果到液化器101的低压氮气供应流100处于足够高的压力以将低压氮气供应流100直接地提供到再循环压缩器118的抽吸部内，则该供应压缩器106还可被消除，并且在那种情况下，加温容器闪蒸和沸腾蒸气流102可通过阀排放到大气内，以简单地控制液体存储容器170的压力。
在令人惊奇的和未预料到的结果的情况下，申请人发现如果高压密相流164通过在换热器130中相对回收的组合蒸气流174间接换热而被冷却到排出流160的温度之下，则高压密相流164的压力到排出流160的压力的减小将不会导致显著量的闪蒸蒸气的生成，因而，液化器101的效率不由消除额外的分离器和它的相关构件而减小。实际上，本领域技术人员将理解，该示范性实施例消除对分离器和过冷却器(例如图3的分离器304和过冷却器310)的需要，同时维持高水平的效率。例如，尽管传统系统和工艺可使用两个或更多个分离器，以在高压和减小的压力处回收闪蒸蒸气，但是公开的系统和工艺在减去显著资本成本和显著运输计划后实现相同的结果，同时实现相等或更好效率。
在另一实施例中，并且如图2所示，公开了与图1相似的系统和工艺；然而该实施例包括不同膨胀器布置。在该系统/工艺中，来自再循环压缩器后冷却器122的流124分成两种流226和228，其供应并行布置的温压伸器238和冷压伸器246的压缩器端。温压伸器238和冷压伸器246的相应出口流240和248在作为流252被供应到换热器130之前组合成流249并且在后冷却器250中冷却。流252在被分成流232和253之前，在换热器130中被冷却到第一中间温度。
流232在温膨胀器234中膨胀以形成流236并且与温排出流160组合，从而在换热器130的中间位置处形成流162。流253被进一步冷却到第二中间温度并且又分成成流256、254。流256在冷膨胀器258中膨胀，以形成排出流160。排出流160然后在换热器130中加温。流254在换热器130中进一步冷却，以形成高压密相流164，其经由膨胀装置166被供应到液体存储容器170。
图3为具有与图1所示的相同膨胀器构造的先前公开的现有技术工艺的流程图，但是其中该工艺不包括从容器回收闪蒸蒸气或沸腾。图3被提供用示范性目的并且用来与图1的系统和工艺相比较。
如在图3中所示，冷端分离器304和过冷却器310合并到液化器301中并且不存在从液体存储容器170回收闪蒸或沸腾蒸气。来自换热器130的冷端的高压密相流164在压力方面在一个或多个膨胀装置300中减小并且所得的两相流302然后连同可包含某些液体的冷膨胀器排出流160一起被供应到分离器304。来自分离器304的蒸气流306在换热器130中加温到中间温度，其中它与温膨胀器排气流136组合，以形成流162。来自分离器304的液体流308在过冷却器310中过冷却到大约78K，以形成流312。过冷液体流312的一部分316在一个或多个膨胀装置318中在压力方面减小并且然后在过冷却器310中蒸发以形成蒸气流320并且在换热器130中再加热以形成流102。过冷液体流312的剩余部分314经由一个或多个膨胀装置166而被供应到液体存储容器170，以形成流168，其中流168被供应到液体存储容器170内。来自液体存储容器170的闪蒸和沸腾蒸气经由流176通过膨胀装置178排放，以形成流180(待排放到大气)以控制容器压力。
图4为示出用于将图1的液化器系统和工艺与ASU或氮气生成器相集成的多个示范性选择的流程图。例如，来自ASU的温端的低压氮气供应流100可由可选供应流400、404或408中的一个或多个完全地或部分地替换。
来自ASU或氮气生成器的温端的高压氮气流400也可与来自供应压缩器后冷却器110的流112混合，以形成流402，其可然后与流114混合，以形成流116，其被供应到再循环压缩器118。可选地，流400可在流114与流112组合的地方的下游混合，或者混合到供应压缩器106或再循环压缩器118的级间位置内。
来自在ASU的冷端处的低压塔或过冷却器的低压氮气流404可与来自液体存储容器170的返回低压流174混合，以形成流406，其然后在换热器130中加热。
来自ASU或氮气生成器的高压塔或单一塔氮气生成器的单一塔的冷高压氮气流408可与来自冷膨胀器158的排出流160混合，以形成流410，其然后在换热器130中加热。
另外地，来自液化器的冷端的高压密相流164的分开部分流412可被直接地供应到ASU或氮气生成器，以提供制冷，同时剩余部分414可被供应到液体存储容器170。如在此使用，流的“分开部分”应意指具有与它从其处获取的流相同的化学成分的部分。分开部分流412可被供应到例如ASU的高压(HP)塔、低压(LP)塔，过冷却器，或换热器。
实例
表1和2提供用于图1和图3的构造/工艺的示范性流动速率，温度、和压力。在图1中公开的构造/工艺导致表1的数据，其中300吨每天的液体氮气在液体存储容器170中产生，该构造/工艺消耗大约5950kW的电。
在图3中公开的构造/工艺导致表2的数据，其中300吨每天的液体氮气也在液体存储容器170中产生。该构造/工艺消耗大约6000kW的电。
重要地，图1/表1的示范性工艺在液体存储容器中产生相同净量(446千摩尔/小时)的液体氮气，但是比先前公开的图3/表2的工艺使用少0.8%的功率，具有低3%的供应速率(流100)，这是由于从液体存储容器回收闪蒸和沸腾蒸气(流174)和到大气的容器沸腾损失的消除(流176)，并且由于第一分离器、第二分离器或过冷却器、和它们相关的阀、控制器和隔离封壳的消除而提供显著资本成本节省。因为液化器的冷部基本上包括仅仅换热器和相关管道系统，所以液化器设备可被直接地隔离并且可消除需要用于包含并且隔离第一分离器、第二分离器或过冷却器、和它们相关的阀、控制器的分离冷箱结构，因而显著减小冷箱的尺寸。当处理并且安排运输路线时减小冷箱的尺寸要求特别重要，这是因为对于更大的预隔离负载(即冷箱负载)某些目的地位置可难以或甚至不能达到。
尽管本发明的方面结合各种图的优选实施例而描述，但是应理解，其它相似实施例可被使用或可对描述的实施例作出更改和添加用于执行本发明的相同功能而不与其背离。因此，本主张权利的发明不应当限于任何单一实施例，而是相反应当根据所附权利要求在宽度和范围方面解释。

Claims (15)

1.一种用于使气体液化的工艺，其包括：
将供应流引入到至少包括温膨胀器和冷膨胀器的液化器内；
将所述供应流在所述液化器中压缩到大于它的临界压力的压力并且将压缩供应流冷却到低于它的临界温度的温度，以形成高压密相流；
从所述液化器移除所述高压密相流并且在膨胀装置中减小所述高压密相流的压力，以形成所得两相流并且然后将所述所得两相流直接地引入到存储容器内；并且
将所述所得两相流的闪蒸部分与来自所述存储容器中的液体的沸腾蒸气组合，以形成组合蒸气流，其中，所述高压密相流的温度低于所述冷膨胀器的排出流的温度。
2.根据权利要求1所述的工艺，其特征在于，所述高压密相流通过相对组合蒸气流间接换热而被冷却到所述排出流的温度之下。
3.根据权利要求1所述的工艺，其特征在于，还包括将所述组合蒸气流的至少部分加热到环境温度。
4.根据权利要求3所述的工艺，其特征在于，还包括将加温的组合蒸气流与所述供应流混合用于再循环。
5.根据权利要求3所述的工艺，其特征在于，还包括将加温的组合蒸气流排放到大气，以控制所述存储容器的压力，其中所述存储容器的压力小于1.5巴。
6.根据权利要求1所述的工艺，其特征在于，还包括从所述存储容器移除所述组合蒸气流的至少部分，在一个或多个膨胀装置中减小所述组合蒸气流的压力以形成低压组合蒸气流，并且将所述低压组合蒸气流排放到大气，以控制所述存储容器的压力，其中所述存储容器的压力小于1.5巴。
7.根据权利要求1所述的工艺，其特征在于，所述供应流为来自空气分离单元的温端的低压氮气供应流。
8.根据权利要求1所述的工艺，其特征在于，还包括在加热之前将来自空气分离单元的低压塔或过冷却器的低压氮气流与来自所述存储容器的组合蒸气流混合。
9.根据权利要求1所述的工艺，其特征在于，还包括从所述液化器获取所述高压密相流体的分开部分，将所述高压密相流体的分开部分直接地供应到空气分离单元或氮气生成器，以提供制冷。
10.根据权利要求9所述的工艺，其特征在于，所述高压密相流体的分开部分在压力方面减小并且被供应到空气分离单元的高压(HP)塔、低压(LP)塔、过冷却器、或主换热器。
11.一种用于使大气气体液化的系统，其包括：
用于接收供应流的第一导管；
液化器，其流体地连接到所述第一导管用于压缩并且冷却所述供应流，以形成高压密相流体，其中，所述液化器至少包括温膨胀器、冷膨胀器、用于将所述供应流压缩到大于它的临界压力的压力的压缩器、和用于将压缩供应流冷却到低于它的临界温度的温度的换热器；
第二导管，其流体地连接到所述液化器用于从所述液化器接收所述高压密相流；
第一膨胀装置，其流体地连接到所述第二导管，以减小所述高压密相流的压力，以形成所得两相流；
第三导管，其流体地连接到所述第一膨胀装置用于接收两相膨胀流；和
存储容器，其流体地连接到所述第三导管用于接收并且存储所述两相膨胀流，
其中，所述存储容器设计成在处于或低于1.5巴的压力处操作，并且其中，所述换热器设计成使得所述高压密相流的温度低于所述冷膨胀器的排出流的温度。
12.根据权利要求11所述的系统，其特征在于，所述存储容器直接地连接到所述第三导管，并且其中，所述第一膨胀装置直接地连接到所述第二导管。
13.根据权利要求11所述的系统，其特征在于，还包括第四导管，其流体地连接到所述存储容器用于接收组合蒸气流，其包括所述所得两相流的闪蒸蒸气部分和来自所述存储容器中的液体的沸腾蒸气部分。
14.根据权利要求13所述的系统，其特征在于，所述第四导管流体地连接到所述换热器和所述第一导管。
15.根据权利要求13所述的系统，其特征在于，还包括第二膨胀装置，其流体地连接到所述第四导管，以减小所述组合蒸气流的压力，以控制所述存储容器的压力。
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