CN105241178B - 用于通过低温分离空气获取压力气体产物的方法和装置 - Google Patents

用于通过低温分离空气获取压力气体产物的方法和装置 Download PDF

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CN105241178B
CN105241178B CN201510388744.XA CN201510388744A CN105241178B CN 105241178 B CN105241178 B CN 105241178B CN 201510388744 A CN201510388744 A CN 201510388744A CN 105241178 B CN105241178 B CN 105241178B
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pressure
air
partial stream
stream
heat exchanger
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CN105241178A (zh
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D·戈卢贝夫
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • 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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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
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Abstract

本发明涉及一种通过在蒸馏塔***中低温分离空气获取压力气体产物(72；73)的方法和装置，蒸馏塔***具有一高压塔(21)和一低压塔(22)。进料空气在主空气压缩机(2)中被压缩至第一压力。第一产物流(69；75)从蒸馏塔***中取出并加压至第一产物压力。第一产物流在第一产物压力下在主热交换器中被蒸发和加热。被加热的第一产物流(72；77)作为压力气体产物(GOX IC；GAN IC)被获取。第三部分流(37)在第二空气涡轮机(38)中被降至比高压塔(21)运行压力高至少1bar的压力。做功降压的第三部分流的第一部分(339)被继续冷却、液化并接下来降压和导入蒸馏塔***中。

Description

用于通过低温分离空气获取压力气体产物的方法和装置
技术领域
本发明涉及一种通过低温分离空气可变地获取压力气体产物的方法和装置。
背景技术
用于空气低温分离的方法和装置例如从豪森/林德，低温技术，第二版1985，第4章(第281至337页)中公开。
这类设备的蒸馏塔***能够被构造成双塔***(譬如作为经典的林德双塔***)，或者也能被构造成三塔或多塔***。除了用于氮氧分离的蒸馏塔之外，所述蒸馏塔***还能够具有其它用于获取高纯度产物和/或其它空气组分尤其是稀有气体的装置，例如氩获取装置和/或氪氙获取装置。
作为“冷凝器-蒸发器”指的是一热交换器，在该热交换器中，第一冷凝流体流与第二蒸发流体流进行间接热交换。每个冷凝器-蒸发器具有一液化室和一蒸发室，所述液化室和蒸发室由液化通道或蒸发通道组成。在所述液化室中执行所述第一流体流的冷凝(液化)，在所述蒸发室中执行所述第二流体流的蒸发。蒸发室和液化室由这些通道的组构成，它们相互处于热交换关系中。冷凝器-蒸发器的蒸发室能够被构造成浴槽式蒸发器、降膜蒸发器或者强制流动蒸发器。
在本发明的过程中，一液态带压的产物流相对一热载体被蒸发并最后作为内部压缩的压力气体产物被获取。该方法也被称为内部压缩。所述方法用于获取气态压力产物。对于超临界压力的情况而言，不发生实际意义上的相变，所述产物流于是被“伪蒸发”。所述产物流譬如可以是一来自一双塔***低压塔的氧产物或者一来自一双塔***高压塔或者主冷凝器液化室的氮产物，通过所述产物流，高压塔和低压塔处于热交换式连接。
相对所述(伪)蒸发的产物流，一处在高压下的热载体被液化(或者，如果所述热载体处在超临界压力下，则被伪液化)。所述热载体常由空气的 一部分构成，在当前情况下由所述被压缩的进料空气的所述“第二部分流”构成。
内部压缩方法譬如从DE 830805，DE 901542(＝US 2712738/US2784572)，DE952908，DE 1103363(＝US 3083544)，DE 1112997(＝US3214925)，DE 1124529，DE 1117616(＝US 3280574)，DE 1226616(＝US3216206)，DE 1229561(＝US 3222878)，DE 1199293，DE1187248(＝US3371496)，DE 1235347，DE 1258882(＝US 3426543)，DE 1263037(＝US3401531)，DE 1501722(＝US 3416323)，DE 1501723(＝US 3500651)，DE253132(＝US4279631)，DE 2646690，EP 93448 B1(＝US 4555256)，EP384483 B1(＝US 5036672)，EP505812 B1(＝US 5263328)，EP 716280 B1(＝US 5644934)，EP 842385 B1(＝US5953937)，EP 758733 B1(＝US 5845517)，EP 895045 B1(＝US 6038885)，DE 19803437A1，EP 949471 B1(＝US6185960 B1)，EP 955509 A1(＝US 6196022 B1)，EP 1031804 A1(＝US6314755)，DE 19909744 A1，EP 1067345 A1(＝US 6336345)，EP 1074805 A1(＝US6332337)，DE 19954593 A1，EP 1134525 A1(＝US 6477860)，DE10013073 A1，EP 1139046A1，EP 1146301 A1，EP 1150082 A1，EP 1213552A1，DE 10115258 A1，EP 1284404 A1(＝US2003051504 A1)，EP 1308680 A1(＝US 6612129 B2)，DE 10213212 A1，DE 10213211 A1，EP 1357342 A1或者DE 10238282 A1DE 10302389 A1，DE 10334559 A1，DE 10334560 A1，DE 10332863 A1，EP 1544559 A1，EP 1585926 A1，DE 102005029274 A1EP1666824 A1，EP1672301 A1，DE 102005028012 A1，WO 2007033838 A1，WO 2007104449 A1，EP 1845324A1，DE 102006032731 A1，EP 1892490 A1，DE 102007014643 A1，A1，EP 2015012 A2，EP2015013 A2，EP 2026024 A1，WO 2009095188 A2或DE 102008016355 A1中被公开。
本发明涉及尤其是这样的***，在这些***中，所有的进料空气被压缩至一压力，该压力明显高于作用在所述蒸馏塔***的塔内部的最高蒸馏压力(通常情况下其即为高压塔压力)。这样的***也被称为HAP过程(HAP表示高空气压力)。在此，所述“第一压力”，即其中压缩总空气的所述主空气压缩机(MAC＝主空气压缩机)的出口压力，譬如比所述最高蒸馏压力高多于4bar，尤其是6至16bar。绝对地，所述“第一压力”譬如介于17至25bar之间。在HAP方法中，所述主空气压缩机一般是唯一由外部能量 驱动的、用于压缩空气的机器。“唯一的机器”在这里被理解为一单级或多级压缩机，所述单级或多级压缩机的所有级与同一个驱动装置连接，其中，所有的级被布置在同一壳体中或者与同一个传动装置连接。
这类HAP方法的替换方案是所谓的MAC-BAC方法，在所述MAC-BAC方法中，空气在所述主空气压缩机中被压缩至相对低的总空气压力，譬如被压缩至所述高压塔的运行压力(加上线路损耗)。来自所述主空气压缩机的空气的一部分在一用外部能量驱动的空气再压缩机(BAC＝增压空气压缩机)中被压缩至一较高的压力。在较高压力下的该空气部分(通常被称为节流流)提供了所述主热交换器中用于(伪)蒸发所述被内部压缩的产物所需热的大部分。所述空气部分在所述主空气压缩机的下游在一节流阀或者一液体涡轮机(DLE＝稠密液体膨胀机)中被降压至在所述蒸馏塔***中所需的压力。
本文开始所提到的类型的具有串联的第一再压缩机(热增压机)和第二再压缩机(冷增压机)的方法从DE 102010055448A1中被公开。
发明内容
本发明的任务在于在能源效率方面继续改善这类方法。
该任务通过权利要求1的特征得以解决。除了所述“第二部分流”-处于特别高的第三压力下的节流流-之外，一另外的节流流在一相对低的压力下，譬如7至15bar，尤其是10至13bar下***纵通过所述主热交换器的冷部分。这一另外的节流流由空气的所述“第三部分流”在其降压部的下游在所述第二空气涡轮机中构成。在所述主热交换器的冷部分中的附加空气流能够实现有利的热交换图进而节省能量，尤其是当氮作为被内部压缩的产物在7和15bar之间获得时。
在许多情况下，可能通过以下方式继续优化所述主热交换器中的热交换过程，即，在主空气压缩机中被压缩的空气的第四部分流在所述第一压力，即所述主空气压缩机的出口压力下在所述主热交换器中被冷却并接下来降压并导入所述蒸馏塔***中。
两个涡轮机流中的一个或两个能够和所述第二部分流一起在所述第一再压缩机中被再压缩至所述第二压力，就像权利要求3和4所述那样。
尤其是所述第三部分流也能够在没有再压缩的情况下保留；它然后在 所述第一压力下被导入所述第二空气涡轮机中。
当该***应当短时地用特别低的液体产量或者作为纯气体设备***纵时，有利的是，在这些时候不将所述做功降压的第三部分流的第二部分导入所述主热交换器中，而是导入所述高压塔的底部蒸发器的液化室中，所述底部蒸发器被构造成冷凝器-蒸发器。
在所述高压塔的底部蒸发器的蒸发室中被至少部分地冷凝的流于是优选在一中间部位上被供应给所述高压塔。
附图说明
下面借助在图1和2中示意性示出的实施例对本发明及本发明的其它细节做更详细的说明。
图1示出了本发明的第一实施例；
图2示出了本发明的第二实施例；
图3示出了本发明的第三实施例。
在图1中，大气空气(AIR)通过一过滤器1被一主空气压缩机2抽吸。所述主空气压缩机在该例中具有五个级并将所述总空气流压缩至譬如19.7bar的“第一压力”。在所述主空气压缩机2下游上的总空气流3在所述第一压力下在一预冷却部4中被冷却。被预冷却的总空气流5在一清洁装置6中被清洁，所述清洁装置尤其是由一对可切换的分子筛吸收器构成。所述被清洁的总空气流7的第一部分8在一热运行的具有再冷却器10的空气再压缩机9中被再压缩至譬如24bar的“第二压力”并接下来被分成“第一部分流”11(第一涡轮机空气流)和“第二部分流”12(第一节流流)。
所述第一部分流11在一主热交换器13中被冷却至大致135K的第一中间温度。被冷却的第一部分流14在第一空气涡轮机15中从所述第二压力做功降压至约5.5bar。所述第一空气涡轮机15驱动热的空气再压缩机9。做功降压的第一部分流16被导入一分离器(相分离器)17中。所述液态部分18经由线路19和20被导入所述蒸馏塔***的所述低压塔22中。
所述蒸馏塔***具有一高压塔21、所述低压塔22和一主冷凝器23以及一常规的具有粗氩塔25和纯氩塔26的氩获取装置24。所述主冷凝器23被构造成冷凝器-蒸发器，在该具体实施例中被构造成级联蒸发器。所述高压塔顶层处的运行压力在该实施例中为5.3bar，所述低压塔顶层处的运行压力为1.35bar。
所述进料空气的所述第二部分流12在所述主热交换器13中被冷却至一高于所述第一中间温度的第二中间温度，经由线路27被供应给一冷压缩机28并在那里被再压缩至大致35bar的“第三压力”。所述被再压缩的第二部分流29在一高于所述第二中间温度的第三中间温度下又被导入所述主热交换器13中并在那里被冷却直至冷端部。所述冷的第二部分流30在一节流阀31中被降压至约所述高压塔的运行压力并经由线路32被供应给所述高压塔21。一部分33又被取出，在一过冷却逆流器34中被冷却并经由线路35和20被馈入所述低压塔22中。
所述进料空气的“第三部分流”436在所述第二压力下被导入所述主热交换器13中并在那里被冷却至第四中间温度，所述第四中间温度在该实施例中稍微高于所述第一中间温度。被冷却的第三部分流37在第二空气涡轮机38中从所述第一压力做功降压。做功降压的涡轮机流339具有这样的压力，该压力比所述高压塔的运行压力高至少1bar，尤其是4至10bar，和这样的温度，该温度比所述热交换器冷端部处的低压氮流55，61的入口温度高至少10K，尤其是15至40K。该流然后在所述热交换器的冷部分中被继续冷却。被继续冷却的第三部分流340作为第三节流流在一节流阀341中被降压至约高压塔压力并经由线路32被导入所述高压塔中。由此可以继续优化所述主热交换器中的热交换进程，尤其是在GAN-IC压力相对低的情况下，譬如为7至15bar，尤其是约12bar时。
所述第二空气涡轮机38驱动所述冷压缩机28。所述做功降压的第三部分流339经由线路40在底部上被供应给的所述高压塔21。
(划分成相同压力的部分流也可以偏离于图1中示图所示在所述主热交换器13的内部执行。)
“第四部分流”41(第二节流流)在所述第一压力下从所述热端部直至所述冷端部通流所述主热交换器13。冷的第四部分流42在一节流阀43中被降压至约所述高压塔的运行压力并经由线路32被供应给所述高压塔21。
所述高压塔21的富氧的底部液体44在所述过冷却逆流器34中被冷却并经由线路45被导入选用的氩获取装置24中。由此产生的蒸汽46和剩余液体47被馈入所述低压塔22中。
所述高压塔21的顶层氮48的第一部分49在所述主冷凝器23的液化 室中相对在蒸发室中蒸发的、来自所述低压塔底部的液态氧被完全或基本完全液化。在此产生的液态氮50的第一部分51作为回流被送至所述高压塔21。第二部分52在所述过冷却逆流器34中被冷却，经由线路53被馈入所述低压塔22中。所述液态低压氮53的至少一部分用作所述低压塔21中的回流；另一部分54能够作为液态氮产物(LIN)被获取。
从所述低压塔22的一中间部位去除气态不纯氮61，在所述过冷却逆流器34和所述主热交换器13中进行加热。所述热的不纯氮62能够被吹入63大气(ATM)中和/或作为再生气体64被用于所述清洁装置6。所述低压塔22顶层的气态氮55同样在所述过冷却逆流器34和所述主热交换器13中被加热并经由线路56作为低压氮产物(GAN)被去除。
线路67和68(所谓的氩通道)使所述低压塔21连接所述氩获取装置24的粗氩塔25。
所述低压塔21底部的液态氧69的第一部分70作为“第一产物流”被去除，在氧泵71中被带至一譬如37bar的“第一产物压力”并在所述第一产物压力下在所述主热交换器13中被蒸发并最终经由线路72作为“第一压力气体产物”(GOX IC——被内部压缩的气态氧)被获取。
可能地，所述低压塔21底部的液态氧69的第二部分73在所述过冷却逆流器34中被冷却并经由线路74作为液态氧产物(LOX)被获取。
在该实施例中，来自所述高压塔21或所述主冷凝器23的液态氮50的第三部分75也经历内部压缩，通过这种方式，即，所述第三部分在氮泵76中被带至譬如12bar的第二产物压力，在所述第二产物压力下在所述主热交换器13中被伪蒸发并最终经由线路77作为被内部压缩的气态氮压力产物(GAN IC)被获取。
所述高压塔21的气态顶层氮48的第二部分78在所述主热交换器中被加热并经由线路79或者作为气态中间压力产物被获取或者-如所示那样-作为密封气(英文Sealgas)被用于所述过程泵中的一个或多个过程泵。
图2与图1的区别在于，所述进料空气的第三部分流36在所述第一压力下被导入所述主热交换器13中并且所述第二涡轮机38因此具有一相应较低的入口压力。
在图3的实施例中，所述高压塔具有一底部蒸发器351。该底部蒸发器尤其是当至少短时地需要特别低的气体产量或者甚至纯气体运行时才投入 使用。前述实施例的涡轮机38不能采用其最大通过量***纵，因为否则必须操纵过多的空气作为第三部分流通过所述主热交换器的所述冷端部并且所述主热交换器的运行因此会不那么有效率。
在图3中，来自所述涡轮机38的第三部分流的一部分350现在能够在特别低的液体产量的情况下被引导绕过所述主热交换器。所述涡轮机38(以及与之耦合的冷压缩机)于是能够采用全部通过量***纵，而不使所述主热交换器中的热交换进程负载。所述流350在所述底部蒸发器351的蒸发室中至少部分被冷凝并接下来经由线路352在一中间部位上被供应给所述高压塔。它由此加强了所述高压塔的下面部分中的蒸馏。
与图3中所示不同，所述流350也能够在被导入所述底部蒸发器之前在所述主热交换器中被冷却至露点状态(Tauzustand)。这可以在一单独的通道中进行，但也经过在适当部位上的中间取出和相应的馈送。

Claims (13)

1.通过在蒸馏塔***中低温分离空气获取压力气体产物(72；73)的方法，所述蒸馏塔***具有一高压塔(21)和一低压塔(22)，在所述方法中，
-所有的进料空气在一主空气压缩机(2)中被压缩至第一压力，所述第一压力比所述高压塔(21)的运行压力高至少4bar；
-在所述主空气压缩机(2)中被压缩的进料空气(7)的第一部分流(8，11，14)在一主热交换器(13)中被冷却至一中间温度并在第一空气涡轮机(15)中做功降压；
-做功降压的第一部分流(16)的至少一个第一部分被导入(40；18，19，20)所述蒸馏塔***中；
-在所述主空气压缩机(2)中被压缩的进料空气的第二部分流(12，27，29，30)在一第一再压缩机(9)中被再压缩至高于所述第一压力的第二压力，在所述主热交换器(13)中被冷却至一中间温度，在一作为冷压缩机被运行的第二再压缩机(28)中被再压缩至高于所述第二压力的第三压力，在所述主热交换器(13)中被冷却并接下来降压(31)和导入(32)所述蒸馏塔***中；
-在所述主空气压缩机(2)中被压缩的进料空气(7)的第三部分流(436，37)在所述主热交换器(13)中被冷却至一中间温度并在第二空气涡轮机(38)中做功降压；并且
-做功降压的第三部分流的至少一个第一部分(339)被导入(340)所述蒸馏塔***中；
-第一产物流(69；75)被液态地从所述蒸馏塔***中取出并加压(71；76)至第一产物压力；
-所述第一产物流在所述第一产物压力下在所述主热交换器(13)中被蒸发或伪蒸发和加热；并且
-被加热的第一产物流(72；77)作为第一压力气体产物被获取，
其特征在于，
-在所述主热交换器(13)中冷却至中间温度的所述第三部分流(37)在所述第二空气涡轮机(38)中被降压至一压力，该压力比所述高压塔(21)的运行压力高至少1bar；
-所述第一空气涡轮机(15)的入口压力比所述第三压力小至少1bar；并且
-做功降压的第三部分流的至少一个第一部分(339)在所述主热交换器(13)中被继续冷却、液化并接下来降压(341)并导入所述蒸馏塔***中。
2.根据权利要求1所述的方法，其特征在于，在所述主空气压缩机(2)中被压缩的空气(7)的第四部分流(41，42)在所述第一压力下在所述主热交换器(13)中被冷却并接下来降压(43)并导入所述蒸馏塔***中。
3.根据权利要求1或2所述的方法，其特征在于，所述第一部分流与所述第二部分流一起在所述第一再压缩机(9)中被带至所述第二压力并在所述第二压力下被导入所述第一空气涡轮机(15)中。
4.根据权利要求1或2所述的方法，其特征在于，所述第三部分流与所述第二部分流一起在所述第一再压缩机(9)中被带至所述第二压力并在所述第二压力下被导入所述第二空气涡轮机(38)中。
5.根据权利要求1或2所述的方法，其特征在于，所述第三部分流在所述第一压力下被导入所述第二空气涡轮机(38)中。
6.根据权利要求1或2所述的方法，其特征在于，至少短时地，做功降压的第三部分流的第二部分(350)不被导入所述主热交换器(13)中，而是被导入所述高压塔的底部蒸发器(351)的液化室中，所述底部蒸发器被构造成冷凝器-蒸发器。
7.根据权利要求6所述的方法，其特征在于，在所述高压塔的所述底部蒸发器(351)的蒸发室中被至少部分地冷凝的流(352)在一中间部位上供应给所述高压塔。
8.根据权利要求1或2所述的方法，其特征在于，所述第一再压缩机(9)被所述第一空气涡轮机(15)驱动。
9.根据权利要求1或2所述的方法，其特征在于，所述第二再压缩机(28)由所述第二空气涡轮机(38)驱动。
10.根据权利要求1或2所述的方法，其特征在于，所述第三部分流与所述第二部分流一起并且与所述第一部分流一起在所述第一再压缩机(9)中被带至所述第二压力并在所述第二压力下被导入所述第二空气涡轮机(38)中。
11.用于通过低温分离空气获取压力气体产物(72；73)的装置，其具有
-一蒸馏塔***，所述蒸馏塔***具有一高压塔(21)和一低压塔(22)；
-一主空气压缩机(2)，用于将所有的进料空气压缩至第一压力，所述第一压力比所述高压塔(21)的运行压力高至少4bar；
-用于使在所述主空气压缩机(2)中被压缩的进料空气(7)的第一部分流(8，11，14)在一主热交换器(13)中冷却至一中间温度的器件；
-用于使被冷却至所述中间温度的第一部分流导入第一空气涡轮机(15)中的器件；
-用于使在所述第一空气涡轮机(15)中做功降压的第一部分流(16)导入所述蒸馏塔***中的器件(40；18，19，20)；
-一第一再压缩机(9)，所述第一再压缩机用于使在所述主空气压缩机(2)中被压缩的进料空气的第二部分流(12，27，29，30)再压缩至第二压力，所述第二压力高于所述第一压力；
-用于使被再压缩的第二部分流在所述主热交换器(13)中冷却至一中间温度的器件；
-一第二再压缩机(28)，所述第二再压缩机作为冷压缩机被运行，所述第二再压缩机用于使所述第二部分流再压缩至第三压力，所述第三压力高于所述第二压力；
-用于使继续再压缩的第二部分流在所述主热交换器(13)中冷却并用于接下来降压(31)并导入(32)所述蒸馏塔***中的器件；
-用于使在所述主空气压缩机(2)中被压缩的进料空气(7)的第三部分流(436，37)在所述主热交换器(13)中冷却至一中间温度的器件；
-一第二空气涡轮机(38)，用于使被冷却的第三部分流做功降压；
-用于使做功降压的第三部分流导入(340)所述蒸馏塔***中的器件；
-用于使第一产物流(69；75)从所述蒸馏塔***中液态取出的器件；
-用于使液态取出的第一产物流(69；75)加压(71；76)至第一产物压力的器件；
-用于使所述第一产物流在所述第一产物压力下在所述主热交换器(13)中蒸发和伪蒸发的器件；并且具有
-用于使被加热的第一产物流(72；77)作为第一压力气体产物被获得的器件，
其特征在于，设置有：
-调节器件，用于使所述第二空气涡轮机(38)的出口压力调节至一压力，该压力比所述高压塔(21)的运行压力高至少1bar；
-用于在一入口压力下使所述第一部分流导入所述第一空气涡轮机(15)中的器件，所述入口压力比所述第三压力低至少1bar；
-用于使做功降压的第三部分流(399)导入所述主热交换器(13)中用于冷却和液化的器件；和
-用于使被液化的第三部分流降压(341)和导入所述蒸馏塔***中的器件。
12.根据权利要求11所述的装置，其特征在于，所述第一再压缩机由所述第一空气涡轮机(15)驱动。
13.根据权利要求11或12所述的装置，其特征在于，所述第二再压缩机由所述第二空气涡轮机(38)驱动。
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