CN101925790A - 用于低温分离空气的方法和设备 - Google Patents

用于低温分离空气的方法和设备 Download PDF

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CN101925790A
CN101925790A CN2009801033531A CN200980103353A CN101925790A CN 101925790 A CN101925790 A CN 101925790A CN 2009801033531 A CN2009801033531 A CN 2009801033531A CN 200980103353 A CN200980103353 A CN 200980103353A CN 101925790 A CN101925790 A CN 101925790A
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tower
pressure
distillation column
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overhead condenser
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CN101925790B (zh
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A·阿列克谢耶夫
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Linde GmbH
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Abstract

本发明涉及一种用于在蒸馏塔系统中低温分离空气的方法和设备，该蒸馏塔系统具有至少一个高压塔(11)和一个低压塔(12)。该方法具有30％或更多的高的预液化。将进料空气导入到该蒸馏塔系统中。该蒸馏塔系统还包括一个预塔(10)，该预塔的工作压力高于高压塔(11)的工作压力。将进料空气的第一部分流(1)导入到该预塔(10)中。该预塔(10)具有一个塔顶冷凝器(14)，该塔顶冷凝器构造为具有冷凝室和蒸发室的冷凝器-蒸发器。将一个气态馏分(30，31)从该预塔(10)的上部区域导入到所述塔顶冷凝器(14)的冷凝室中。将在所述冷凝室中形成的液体(6)至少部分地作为回流(7)输出给预塔(10)。将进料空气的第二部分流(2a；2b)导入到所述塔顶冷凝器(14)的蒸发室中。

Description

用于低温分离空气的方法和设备
技术领域
本发明涉及一种如权利要求1前序部分所述的用于低温分离空气的方法。
背景技术
用于低温分离空气的方法和设备例如已由豪森/林德的1985年第二版《低温技术》第4章(第281至337页)公开。
本发明的蒸馏塔系统包括用于氮氧分离的双塔系统(例如典型的林德双塔系统)，该双塔系统具有彼此处于热交换关系的高压塔和低压塔。高压塔与低压塔之间的热交换关系通常通过主冷凝器实现，在该主冷凝器中，高压塔的塔顶气体逆着低压塔的蒸发的池底液体液化。该蒸馏塔系统除了用于氮氧分离的塔之外还可具有例如用于获得其它空气组分、尤其是惰性气体的其它设备，例如氩获取设备或氪氙获取设备，所述氩获取设备包括至少一个粗氩塔。所述蒸馏塔系统除了蒸馏塔之外还包括直接配置给所述蒸馏塔的换热器，所述换热器通常构造为冷凝器-蒸发器。
多数的现代空气分离设施是基于所谓的双塔建立的。这个由两个耦联的具有不同工作压力的塔的系统不仅允许获取气态的含氧、含氩和含氮的产品，而且也允许获取液态的馏分。这些液体可以作为液态的最终产品从所述空气分离设施中取出或者被内压缩(在一个泵中加压到较高压力上并且被加热)，从而它们然后可以作为气态的压力产品使用。
如果将这种液态馏分从双塔系统中取出，则必须将相应量的空气在供入到该双塔系统中之前预液化，也就是说，将一部分空气气态地(通往高压塔的进料空气和例如来自拉赫曼透平的、直接供入到低压塔中的空气)导入到该双塔系统中并且将一部分空气液态地(节流流和来自克劳德透平的液态空气，如果存在的话)导入到该双塔系统中。如果液态地取出很多产品，则相应地提高预液化的空气的量。
因为仅仅是两个塔的下部区段被加载液态空气，因此预液化的空气仅仅很少地参与到双塔中的精馏过程中(与液态空气相比)。因此，所述预液化对于双塔中的精馏过程具有负面影响。随着空气预液化的升高，氧产率(以及氩产率，如果该系统生产氩的话)降低。所述空气分离设施的效率和经济性降低。
为了加强精馏(特别是在两个塔的上部区段中)，人们采取所谓的“供料压缩机”等措施(该供料压缩机将来自低压塔上部的产品的一部分压缩到高压塔的压力上，然后将该部分供入到高压塔中)和/或试图使用用于产生冷的所谓氮回路(在此空气不是在双塔之前而是在压力塔内部通过液态氮液化)。然而所述措施意味着较高的能耗并且由于换热器和/或机器数量较高而使得总设施昂贵。
发明内容
本发明的任务在于，即使在高的预液化(例如总进料空气的30摩尔％以上、特别是40摩尔％以上)的情况下也可以在不使用附加的机器和换热器的情况下提高空气分离设施的氧产率(和氩产率，如果获取氩的话)。
所述任务通过权利要求1的特征解决。在此，在传统双塔上游连接一个附加的第三塔(“预塔”)。液态空气的至少一部分(“第一部分流”)首先被导入到该第三塔中并且(类似于在双塔的高压塔中)被分离为液态氮馏分和粗氧。所述连接在上游的塔借助于一个塔顶冷凝器(通常安置在塔上方)用预液化的空气(“第二部分流”)冷却。所述液态空气在此蒸发并且被气态地供入到蒸馏塔系统、特别是供入到高压塔中。
第三塔以一个高于双塔的高压塔压力的压力工作，从而在塔顶冷凝器中蒸发的空气可被导入到高压塔中。
预塔与高压塔之间的压力比(分别在塔顶测量)优选为至少1.4并且特别是在1.4与1.8之间、优选在1.5与1.7之间。
然后，将来自预塔(或来自预塔的塔顶冷凝器的冷凝室)的液态氮供入到高压塔中，将来自预塔的下部区域的液态粗氧导入到高压塔和/或低压塔中，或者如果存在氩部分的话替代或附加地导入到氩部分中。
通过这种布置实现了下述优点：
-预液化的空气在预塔的塔顶冷凝器中蒸发并且气态地导入到双塔中。从而显著降低预液化的负面效应。
-双塔中的精馏可通过一个或多个来自预塔或预塔的塔顶冷凝器的洗涤-LIN馏分得到改善。
-氧产率显著提高，从而即使在高于50％的预液化的情况下也能实现通常的产率。对于氩产率也是这样，如果所述设施附加地产生氩的话。
-塔的尺寸、特别是高压塔和预塔的尺寸相对小。
-从所述预塔中可取出比双塔的高压塔的压力高的压力氮(VHPGAN-very high pressure gaseous nitrogen)。
-为了产生冷，可将空气在透平中不仅膨胀到低压塔的压力(拉赫曼透平)或高压塔的压力(HDS克劳德透平)，而且可膨胀到预塔或预塔的塔顶冷凝器的压力(VS克劳德透平)。
根据本发明的基本构思，尽可能将所有可在高压下提供的、适合于冷却预塔的过程流用来进行冷却(但是这不排除在个别情况下将所述过程流的一部分在其他部位上导入到蒸馏塔系统中)。特别是优选将全部预液化的空气、在任何情况下将预液化空气的80摩尔％以上或90摩尔％以上导入到预塔的塔顶冷凝器的蒸发室中。
此外，本发明还涉及一种如权利要求12所述的用于低温分离空气的设备。
在本发明的范围内，下列变型方案都是可以的并且必要时也可以彼此组合：
1.预塔在双塔旁边(高压塔和低压塔彼此叠置)。
2.所有三个塔彼此并排。
3.三个具有VS克劳德透平的塔，所述VS克劳德透平将气态空气膨胀到预塔中并且将液态空气膨胀到预塔的塔顶冷凝器中。
4.在方法中应用将全部空气压缩到显著高于预塔压力的压缩装置；在此通常将一部分在所谓的内压缩的范围内液化或(在超临界压力下)伪液化并且接着被节流膨胀；其余的在一个或多个透平中做功膨胀，特别是膨胀到预塔或预塔的塔顶冷凝器的压力。
5.三个具有HDS克劳德透平的塔，所述HDS克劳德透平将空气膨胀到高压塔中。
6.三个具有拉赫曼透平的塔，所述拉赫曼透平将空气膨胀到低压塔中。
7.三个塔与两个透平的组合(VS克劳德透平与HDS克劳德透平，VS克劳德透平与拉赫曼透平，HDS克劳德透平与拉赫曼透平)。
8.三个具有三个透平的塔(VS克劳德透平，HDS克劳德透平，拉赫曼透平)。
9.具有或不具有氩获取装置。
10.换热器可以是分开式或集成式的。
附图说明
下面借助于附图中描述的实施例对本发明以及本发明的其它细节进行详细说明。
图1是本发明方法的第一实施例，
图2是第二实施例，同时示出主换热器和作为唯一膨胀机的VS克劳德透平，
图3是图2的一种变型方案，其中，全部的气态进料空气(第一部分流)来自VS克劳德透平，
图4是具有HDS克劳德透平作为唯一膨胀机的第四实施例，
图5是具有拉赫曼透平作为唯一膨胀机的第五实施例，和
图6是用于获得不纯净氧的第五实施例，同时将全部空气压缩到显著高于前塔压力。
具体实施方式
在图1中没有示出供料空气的压缩、净化和冷却。蒸馏塔系统在此包括一个预塔10、一个高压塔11和一个低压塔12以及与其相连的冷凝器-蒸发器，即主冷凝器13和预塔的塔顶冷凝器14。此外，蒸馏塔系统也可选择性地具有一个氩部分15，该氩部分特别是包括至少一个粗氩塔和该粗氩塔的塔顶冷凝器；此外，所述氩部分还可以具有用于氩氮分离的精氩塔。
在该实例中，用于氮氧分离的分离塔具有下述工作压力(分别在塔顶处)：
预塔10.....................7.5至12bar，
高压塔11..................5.0至6.5bar，
低压塔12..................1.3至1.6bar。
进料空气的第一部分流1气态地来自于主换热器的冷端(未示出)或来自于透平。该第一部分流处于稍高于预塔13的工作压力的压力下并且直接在池底的上方被导入。
预塔10具有一个塔顶冷凝器14，空气的第二部分流以液态状态被导入到该塔顶冷凝器的蒸发室中。在该实例中，所述“第二部分流”由两个底流2a、2b构成。底流2a来自VS克劳德透平的出口，底流2b来自所述主换热器的冷端(未示出)并且逆着液态地从该蒸馏塔系统中取出并且接着液态地提高压力的被冷凝或者(在超临界压力下)被伪冷凝。在导入到塔顶冷凝器14的蒸发室中时，第二部分流2a、2b基本上(85至95摩尔％)由液体组成。其液体分量包括总进料空气的30至50摩尔％。其余的进料空气被气态地导入到蒸馏塔系统中。气态导入(除了流体2a、2b和透平流3中可能的气体分量之外)完全地通过将第一部分流1导入到预塔10的内部进行。
此外，在该实例中将一个附加的液态流4导入到所述塔顶冷凝器14的蒸发室中。该液态流来自预塔10的中间部位，该中间部位设置在池底上方的大致8至16理论或实际塔板处。
在此，预塔的全部池底液体5被导入到高压塔11中，确切地说直接在高压塔的池底处被导入。替代或附加地，将预塔的池底液体5或其一部分(在过冷却-逆流器37中冷却之后)供入到低压塔12和/或氩部分15中(图中未示出)。在塔顶冷凝器14的冷凝室中由预塔10的塔顶氮10的一部分31产生的液体6的第一部分作为塔顶回流7供入到预塔10中并且其第二部分8被引导至高压塔11的塔顶。此外，可以将富氮的不纯净馏分9从预塔导入到高压塔中；该不纯净馏分9在预塔10的一个中间部位上(该中间部位设置在塔顶下方的大致8至16理论或实际塔板处)被取出并且在一个中间部位处被引导至高压塔11。
在塔顶冷凝器的蒸发室中形成的、蒸发的馏分16通过管路17与进料空气的来自HDS克劳德透平的出口的第三部分流18一起被引导至高压塔的池底。来自预塔10的塔顶冷凝器14的冲洗液体32在下部区域中的一个中间部位上被供应给高压塔10。
此外，在该实例中将一个另外的液态流4导入到塔顶冷凝器14的蒸发室中。该另外的液态流来自预塔10的一个中间部位，该中间部位设置在池底上方的大致8至16理论或实际塔板处。
此外，双塔11/12/13和可选的氩部分15以普遍公知的方式工作。
从高压塔11中在池底处将液态的粗氧33、在导入冲洗液体32的中间部位处将液态的空气馏分34、从上方远处的中间部位上将不纯净氮35并且将来自主冷凝器13的冷凝室的液态纯氧在一个过冷却-逆流器37中与回流间接热交换的情况下冷却并且通过管路38、39、40或41在合适的部位上导入到低压塔12中。此外，可以将气态的空气42从拉赫曼透平和/或将液态空气43从HDS克劳德透平供入到低压塔12中。
如果该设施没有氩部分，则可取出下列产品：
-从低压塔12的塔顶取出气态氮(GAN)44、45；
-从低压塔12的塔顶取出液态氮(LIN)46；
-从低压塔上部区域中的一个中间部位取出气态的不纯净氮(UN2)47、48；
-直接在低压塔12的池底上方取出气态氧(GOX)49；
-从低压塔12的池底取出液态氧(LOX)50；
-从高压塔11的塔顶取出气态的压力氮(HPGAN)51；
-从主冷凝器13的冷凝室或从高压塔11取出液态的压力氮(HP-LIN)52；
-从预塔10的塔顶取出压力特别高的气态氮(VHPGAN)53；
该设施能够、但不是必须同时产生所述产品。
气态的产品流在一个未示出的主换热器中在与进料空气间接热交换的情况下被加热。主换热器可以由一个单元或由两个或更多并联和/或串联连接的单元组成。液态的氧可以作为液态产品获得；替代或附加地，液态地从低压塔取出的氧的至少一部分在液态下被加压并且接着在所述主换热器中被蒸发或(在超临界压力下)被伪蒸发且被加热，接着作为气态的压力产品被取出(所谓的内压缩)。
在图1实施例的一个变型方案中，该系统具有一个用于获取液态纯氩(LAR)的氩部分15。该氩部分包括一个或多个用于氩氧分离的粗氩塔和一个用于氩氮分离的精氩塔，它们以普遍公知的方式工作。粗氩塔的下端部通过管路61、62与低压塔12的一个中间区域连通。来自高压塔11的液态粗氧在该情况下通过管路33A被导入到所述氩部分中并且特别是至少部分地在粗氩塔的塔顶冷凝器中至少部分地蒸发(未示出)。至少部分地呈气态的粗氧通过管路38A被供入到低压塔12中。此外，从所述氩部分15中还取出气态的剩余流(废弃物)55。
由图1的实施例可得出下列不同于附图的变型方案：
-管路4可被去掉或者保持不工作。于是塔顶冷凝器14仅仅通过液化的空气2a、2b冷却。
-预塔10的池底液体5可以部分地或完全地代替在37中过冷却之后导入到高压塔11中而导入到低压塔12中。如果要获取氩的话，可将一部分或全部过冷却后的液体在导入到低压塔之前用来冷却粗氩塔的塔顶冷凝器。
图2示出主换热器260和一个作为唯一的膨胀机的VS克劳德透平261的图示。所述透平可以要么借助于油制动器262要么借助于发生器要么借助于再压缩机来制动，该再压缩机要么压缩透平流要么压缩节流流2b(在其在主换热器260中[伪]液化的上游)。经透平膨胀和至少部分地液化的空气263被导入到一个相分离装置264中。液态分量264被导入到预塔10的塔顶冷凝器14的蒸发室中。气态分量270与来自主换热器260的气态空气汇合并且通过管路1被供入到预塔10中。
在图2中还示出通过内压缩(internal compression)来获取气态的压力氧293、294。在此，液态氧50的至少一部分(IC-LOX)被从低压塔12的池底通过管路290供应给一个氧泵291、在那里被加压到增高的压力并且其至少第一部分在该增高的压力下在主换热器260中蒸发或伪蒸发并且作为高压产物294被取出。另一部分可以被减压(292)并且在该降低的压力下在主换热器260中蒸发或伪蒸发并且最后作为中间压力产物293被取出。
附加或替代地，能够以类似的方式通过内压缩获取一个或两个压力非常高的氮产物296、297，其方式是，将液态的高压氮52在一个氮泵295中加压到相应高的压力并且在该压力下(且必要时部分地在稍低的中间压力下)在主换热器260中被(伪)蒸发和加热。
图3的实施例与图2的不同之处在于，全部的气态进料空气(“第一部分流”)301均来自于VS克劳德透平361。
图4示出第四实施例，其具有一个HDS克劳德透平465作为唯一的膨胀机。所述透平可以要么借助于油制动器466要么借助于发生器要么借助于再压缩机来制动，该再压缩机要么压缩透平流要么压缩节流流(在其在主换热器260中[伪]液化的上游)。经透平膨胀和至少部分地液化的空气467被导入到一个相分离装置468中。液态分量469通过管路471被导入到低压塔12中。气态分量470与来自预塔10的塔顶冷凝器的气态空气16汇合并且通过管路417被供入到高压塔11中。
在图5的实施例中，一个拉赫曼透平形成唯一的膨胀机。所述透平可以要么借助于油制动器562要么借助于发生器要么借助于再压缩机来制动，该再压缩机压缩透平流(在其在主换热器260中[伪]液化的上游)。经透平膨胀的气态空气563被供入到低压塔12中。
在图6中示出本发明方法的一个变型方案，其特别是适合于获取不纯净氧。在此，所有空气被压缩到显著高于预塔压力。在其他方面该变型方案很大程度上相应于图3的方案。然而在此一般来说氩获取意义不大。
在此，进料空气在主空气压缩机601中加压到例如5.5至24bar的压力、在该压力下被供应给预冷却装置602并且进一步被供应给预净化装置603，该预净化装置例如构造为Molsieb吸收器-站。所有经过净化的空气接着在一个再压缩机604中被进一步压缩到例如高达40bar的压力。由此得到的高压空气605被分为第一支流606和第二支流607。
第一支流606在一个另外的、由VS克劳德透平361驱动的再压缩机661中被加压到更高的压力并且用作节流流2b。第二支流607在所述再压缩机604的出口压力下被导入到主换热器260中并且在VS克劳德透平361中膨胀。
所有图示的过程和设施都应理解为示例性的。附图首先应表示功能性的关系。高压塔和低压塔虽然上下叠置地示出并且具有集成的主冷凝器，但是在本发明的范围内这些塔和冷凝器的任何其他的布置方式都是可以的。
所述塔可以装备有筛塔板、包装(sructured packing)或非调节的填充物(non-structured packing)或者也包括所述类型的物质交换元件的组合。
主冷凝器构造为降膜式蒸发器或浴蒸发器。在浴蒸发器的情况下，其可以单层地或多层地(级联冷凝器)构成。预塔的塔顶冷凝器优选构造为浴冷凝器。
在实际的布置中一些流或塔区段可以缺失。在方法技术方面这意味着：相应流的量等于零或者相关区段中的理论塔板的数量等于零。在设备方面通常这意味着：相应的管路或相应的塔区段缺失。
主换热器可以分别集成地或分开地构成，附图仅仅示出交换器的基本功能——热流通过冷流来冷却。
在本发明的所有实施例中没有使用将液体从一个塔输送到另一个塔的泵。

Claims (13)

1.用于在蒸馏塔系统中低温分离空气的方法，该蒸馏塔系统具有至少一个高压塔(11)和一个低压塔(12)，并且在该蒸馏塔系统中：
-将进料空气导入到该蒸馏塔系统中，其中，
-将进料空气的第一部分气态地导入到该蒸馏塔系统中，并且
-将进料空气的第二部分在液态状态下导入到该蒸馏塔系统中，并且
-所述第二部分包括总进料空气量的至少30摩尔％，
其特征在于，
-该蒸馏塔系统还包括一个预塔(10)，该预塔的工作压力高于高压塔(11)的工作压力，
-将进料空气的第一部分流(1；301)导入到该预塔(10)中，
-该预塔(10)具有一个塔顶冷凝器(14)，该塔顶冷凝器构造为具有冷凝室和蒸发室的冷凝器-蒸发器，
-将一个气态馏分(30，31)从该预塔(10)的上部区域导入到所述塔顶冷凝器(14)的冷凝室中，
-将在所述冷凝室中形成的液体(6)至少部分地作为回流(7)输出给预塔(10)，并且
-将进料空气的第二部分流(2a；2b)至少部分地在液态状态下导入到所述塔顶冷凝器(14)的蒸发室中。
2.根据权利要求1的方法，其中，进料空气的第二部分流(2a；2b)的液态分量在导入到所述塔顶冷凝器(14)的蒸发室中时包括总进料空气量的30摩尔％以上、特别是35摩尔％以上、特别是40摩尔％以上。
3.根据权利要求1或2的方法，其特征在于，所述进料空气的第二部分包括进料空气量的35摩尔％以上、特别是40摩尔％以上。
4.根据权利要求1至3中任一项的方法，其特征在于，将至少一个最终产品流(46；50；52)液态地从所述蒸馏塔系统取出并且将其作为液态产品获得。
5.根据权利要求1至4中任一项的方法，其特征在于，将至少一个液态产品流(50，290；52)从所述蒸馏塔系统取出、在液态状态下将其加压到增高的压力(291；295)并且使其在该增高的压力下通过间接的热交换(206)蒸发或伪蒸发并且最终将其作为气态的产品流(293；294；296；297)取出。
6.根据权利要求1至5中任一项的方法，其特征在于，将全部进料空气在一个或多个空气压缩机(601，604)中压缩到第一压力，该第一压力比高压塔的工作压力高至少1bar。
7.根据权利要求1至6中任一项的方法，其特征在于，将在所述塔顶冷凝器(14)的蒸发室中形成的、蒸发的馏分(16)的至少一部分在预塔(10)的塔顶冷凝器的蒸发室下游导入到所述蒸馏塔系统中、特别是导入到高压塔(11)中。
8.根据权利要求1至7中任一项的方法，其特征在于，将在所述预塔(10)的塔顶冷凝器(14)的冷凝室中形成的液体(6)的至少一部分(8)供入到高压塔和/或低压塔中。
9.根据权利要求1至8中任一项的方法，其特征在于，在低压塔中产生氮含量为至少99摩尔％、特别是99.95摩尔％以上的氮产品。
10.根据权利要求1至9中任一项的方法，其特征在于，将一个含氩的流(61)从低压塔(12)导入到一个氩部分(15)中，该氩部分具有至少一个粗氩塔，从该氩部分(15)中取出氩产品(LAR)。
11.根据权利要求1至10中任一项的方法，其特征在于，所述进料空气的第二部分流(2a；2b)在导入到所述塔顶冷凝器(14)的蒸发室中时具有80至100％、特别是85至95摩尔％的液态分量。
12.用于低温分离空气的设备，
-具有一个蒸馏塔系统，该蒸馏塔系统具有至少一个高压塔(11)和一个低压塔(12)，
-具有用于调节的装置，
-具有用于将进料空气导入到所述蒸馏塔系统中的装置，
-其中，该蒸馏塔系统还具有一个预塔(10)，该预塔的工作压力在该设备工作时高于高压塔(11)的工作压力，
-具有用于将进料空气的第一部分流(1；301)导入到该预塔(10)中的装置，
-其中，该预塔(10)具有一个塔顶冷凝器(14)，该塔顶冷凝器构造为具有冷凝室和蒸发室的冷凝器-蒸发器，
-具有用于将一个气态馏分(30，31)从该预塔(10)的上部区域导入到所述塔顶冷凝器(14)的冷凝室中的装置，
-具有用于将在所述冷凝室中形成的液体(6)作为回流(7)供入到预塔(10)中的装置，并且
-具有用于将进料空气的第二部分流(2a；2b)至少部分地在液态状态下导入到所述塔顶冷凝器(14)的蒸发室中的装置，
-其中，所述用于调节的装置这样构成，使得在该设备工作时
-总进料空气量的至少30摩尔％在液态状态下被导入到所述蒸馏塔系统中。
13.根据权利要求12的设备，其特征在于，所述用于调节的装置这样构成，使得在该设备工作时所述进料空气的第二部分流(2a；2b)的液态分量在导入到所述塔顶冷凝器(14)的蒸发室中时包括总进料空气量的30摩尔％以上。
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