CN107580670B - 通过低温空气分离制备氧的设备 - Google Patents

通过低温空气分离制备氧的设备 Download PDF

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CN107580670B
CN107580670B CN201680027362.7A CN201680027362A CN107580670B CN 107580670 B CN107580670 B CN 107580670B CN 201680027362 A CN201680027362 A CN 201680027362A CN 107580670 B CN107580670 B CN 107580670B
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column
auxiliary
pressure column
condenser
liquid
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CN107580670A (zh
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S·洛赫纳
T·诺伦
L·基希纳
D·戈卢别夫
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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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    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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Abstract

本发明涉及用于通过低温分离空气产生氧的设备。所述设备包括高压塔(1)，低压塔(2)和主冷凝器(3)。氩排出塔(31)与所述低压塔(2)的中间点流体连通，并且与氩排出塔顶部冷凝器(17)相连。辅助塔(140)包括贮槽区域，从所述氩排出塔顶部冷凝器(17)将气体通入所述贮槽区域中。所述辅助塔(140)的顶部与回流液管道(136b)相连，以从所述高压塔或顶部冷凝器引入液体流。所述液体流具有至少与空气相等的氮含量。来自所述高压塔(1)的贮槽的液态粗氧(16c)的至少一部分在第一中间点被送入辅助塔。辅助塔顶部的压力高于低压塔(2)的顶部的压力至少50mbar。

Description

通过低温空气分离制备氧的设备
技术领域
本发明涉及根据权利要求1的前序部分的低温分离空气制备氧的方法。
背景技术
Hausen/Linde(2nd Edition,1985)的专著“Tieftemperaturtechnik”[低温技术]和Latimer在Chemical Engineering Progress(Vol.63,No.2,1967,page 35)一篇文章中特别地描述了通用的低温分离空气的原理和双塔装置的构造。双塔中的高压塔与低压塔之间的热交换关系通常通过主冷凝器来实现，其中来自高压塔的顶部气体通过从低压塔蒸发底部液体而被液化。
本发明的蒸馏塔系统原则上可以配置为具有高压塔和低压塔的经典双塔系统。除了用于氮-氧分离的两个分离塔之外，其还可以包括用于获得其它空气组分，特别是惰性气体的其它装置，例如获得氪-氙的装置。
“氩排出塔”是指用于氩-氧分离的分离塔，其不用于获得纯氩产物，而是用于从在高压塔和低压塔中待分馏的空气中排出氩。它的互连仅仅稍微不同于经典的粗氩塔的互连，但是它包含少得多的理论塔板，即少于40，特别是15-30。类似于粗氩塔，氩排出塔的底部区域连接到低压塔上的中间点，氩排出塔由蒸发侧的顶部冷凝器冷却，其中引入了来自高压塔的经压缩的底部液体；氩排出塔不包括底部蒸发器。
在本发明中，主冷凝器和氩排出塔的顶部冷凝器被配置为冷凝器-蒸发器。术语“冷凝器-蒸发器”是指热交换器，在其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-蒸发器都具有液化空间和蒸发空间，所述液化空间和蒸发空间分别由液化通道和蒸发通道组成。第一流体流的冷凝(液化)发生在液化空间中，第二流体流的蒸发发生在蒸发空间中。蒸发空间和液化空间由处于热交换相互关系中的通道组构成。
主冷凝器可以被配置为单级或多级浴式蒸发器，特别是级联式蒸发器(如例如EP1287302 B1＝US 6748763 B2中所述)，或者降膜式蒸发器。所述冷凝器可以由单个热交换器块形成，或者由布置在常压容器中的多个热交换器块形成。
空气分离设备的蒸馏塔系统布置在一个或多个冷箱中。“冷箱”在本文中被理解为意味着用外壁完全包围绝热内部的绝热外壳；要被绝热的设备部件，例如一个或多个分离塔和/或热交换器，布置在内部。可以通过外壁的适当构造和/或通过用绝热材料填充设备部件和外壁之间的间隙来实现绝缘效果。后一情况优选使用粉状材料例如珍珠岩。不仅在低温空气分离设备中进行氮-氧分离的蒸馏塔系统，还有主热交换器和其它冷设备部件都必须被一个或多个冷箱包围。冷箱的外部尺寸通常决定了预制设备的在途尺寸。
“主热交换器”用于冷却与来自蒸馏塔系统的回流间接热交换的进料空气。所述热交换器可以由单个热交换器部分或多个并联和/或串联连接的热交换器部分形成，例如来自一个或多个板式热交换器块。专门用于单一液体或超临界流体的蒸发或伪蒸发而不加热和/或蒸发另一种流体的独立的热交换器不属于主热交换器。
相对空间术语“顶部”、“底部”、“之上”、“之下”、“上面”、“下面”、“旁边”、“并排”、“垂直”、“水平”等是涉及正常操作中分离塔的空间排列。两个塔或装置部件“一个在另一个之上”的布置在本文中理解为两个装置部件中较下部的部件的上端相对于两个装置部件中较上部的部件的下端位于较低或相同的测量高度处，并且两个装置部件在水平面上的投影重叠。特别地，两个装置部件精确地布置为一个在另一个之上，即两个塔的轴线在相同的垂直直线上排列。
从IPCOM000176762D已知一种开头所述的类型的方法和相应的设备。在图3中示出的是一种空气分离设备，其包括由高压塔和低压塔组成的双塔，所述低压塔包括氩塔和布置在其上的辅助塔。所述辅助塔用于卸载低压塔，因此在与低压塔的相应部分相同的压力下运行。在辅助塔的底部引入低压塔的气体。
发明内容
本发明的目的在于使得开头所述的类型的方法和相应的设备更节能。特别涉及特别大容量的空气分离设备，特别是用于获得氧。这种设备特别地被配置为大于370000Nm3/h，优选大于1 000 000Nm3/h的空气速率。
通过根据本发明的在蒸馏塔系统中通过低温分离空气来制备氧的方法来实现该目的。
在本发明中，来自高压塔的粗氧不进入或不完全进入氩冷凝器的蒸发空间，但是至少一部分，特别是大于10％，优选大于20％供应至中间点处，即至少一个传质部分之上的辅助塔中。
辅助塔顶部的操作压力比低压塔顶部的操作压力高至少50mbar。压力差为例如50-200mbar，优选50-150mbar。因此，来自辅助塔顶部的氮产物具有足够的压力以能够用作空气净化的再生气体。因此，低压塔顶部的压力可以极低。然而，所述压力通过主冷凝器(约3倍)和高压塔来确定全部进料空气需要压缩到的进料空气压力。在低压塔的顶部的减压装置导致高压塔压力显著更高地降低约200-300mbar，从而导致在进料空气的压缩中相当节能。
在辅助塔中，氩排出塔顶部冷凝器(氧含量通常约为32-40mol％)的蒸发馏分在低压塔外部精馏。因此，在低压塔的相关部分中不再进行一部分氮-氧分离，因此相应地降低低压塔的负荷。相反地，在低压塔基本相同的直径和长度下，能够相应地提高容量并且在整个设备中获得更大量的氧。原则上，来自氩排出塔顶部冷凝器的蒸发空间的全部气体可以通入辅助塔并在其中进行精馏。然而，可以仅将该气体的一部分通入辅助塔中，并将剩余部分通过单独的气体导管进入低压塔。还可以将来自低压塔的气体通入辅助塔。在最简单的情况下，本发明的辅助塔精确地包括两个传质部分，其中至少一部分来自高压塔的粗氧供应到两个传质部分之间的中间点；或者，辅助塔包括三个或更多个传质部分。传质部分由规整填料的常规精馏塔板，例如筛板组成或由不同类型的传质单元的组合组成。
辅助塔从高压塔或主冷凝器获得回流。
当来自辅助塔的所有回流液体都被排出到塔底部之上时，用于氩排出塔顶部冷凝器的冷却液体可以仅仅来自高压塔的底部。如果只有一部分回流液体或甚至没有回流液体从辅助塔中排出，则所述液体与来自高压塔底部的冷却液体混合。所述液体可以直接引入到氩排出塔顶部冷凝器的蒸发空间中。或者，所述液体引入到塔底之上的辅助塔中；然后，其通过传质部分流入辅助塔的底部，从而流入氩排出塔顶部冷凝器的蒸发空间。
优选的是从辅助塔获得的气体顶部馏分为与从低压塔的气体顶部氮不同的气体氮产物。由于这种直接产物从辅助塔排出，相应的气体量甚至不引入低压塔，从而减少了所述塔的负荷。“气体氮产物”在本文理解为意指具有比空气更高的氮含量的气体。这可以是还包含0.1-7mol％氧的残余气体。在另一个实施方案中，还可以获得氧含量低至1ppm的技术纯度的氮。
来自氩排出塔顶部冷凝器的蒸发空间的气体原则上可以通过管道进入至辅助塔的底部区域。氩排出塔顶部冷凝器和辅助塔可以布置在两个独立的容器中。然而，当辅助塔和氩排出塔顶部冷凝器被公共容器包围，特别是，氩排出塔顶部冷凝器布置在辅助塔的底部时，通常是更有利的。因此，氩排出塔顶部冷凝器同时是辅助塔的底部蒸发器。
根据本发明的设备还可以包括一个或多个液体管道，用于来自一个或多个中间点或辅助塔底部的的一种或多种液体。这些液体都引入到低压塔中。因此，来自辅助塔的回流液体和/或底部液体作为另外的中间回流引入低压塔中。
当设备具有用于在第二中间点将额外的液体或气体馏分引入辅助塔中的另外的中间进料时，也是有利的。这里，另外的液体馏分，特别是液体空气馏分，在布置在第一中间点上方的第二中间点处引入辅助塔中。可以提供一个或多个这种另外的中间进料，通过其每一个另外的中间进料将相应的气体或液体馏分，例如液体空气引入辅助塔，并且同样参与辅助塔而不是低压塔中的氮-氧分离。这可以是其中氮含量在辅助塔底部/在氩排出塔顶部冷凝器的蒸发空间中的和辅助塔顶部的之间的任何馏分，例如甚至来自涡轮减压的气态空气。每个这样的中间进料还有助于优化低压塔和辅助塔之间的负载分布，以及在低压塔和辅助塔的各个传质部分中达到最佳的液体-蒸气比。特别地，优化了辅助塔中的精馏效率。
在本发明的上下文中，高压塔和低压塔可以并排布置，并且氩排出塔顶部冷凝器和辅助塔可以布置在高压塔的上方。
高压塔和低压塔的并排布置本身是已知的，例如DE 827364或US2762208。与双塔布置相比，这减少了塔的输送长度，并且运输到施工现场的成本较低且复杂度更低。
两塔“并排”的布置应被理解为意味着设备的正常操作中两塔的位置使得它们的横截面在水平面上的投影不重叠。然后两塔的下端通常在相同的测量高度加/减5m。
两塔“一个在另一个之上”或“一个在另一个之下”的布置应被理解为意味着在设备的正常操作中两塔的位置使得它们的横截面在水平面上的投影重叠。例如，当两塔中的一个精确地布置在另一个之上时，两塔的轴在相同的垂直直线上排列。
由于在高压塔上方布置了氩排出塔顶部冷凝器和辅助塔，这些装置不需要额外的建筑面积；设备的占地面积保持不变。即使对于具有高度限制的设备，这种一个在另一个之上的布置也是没有问题的，因为高压塔明显低于低压塔。这种布置从工艺工程的角度来看是有利的，因为主冷凝器上除了对于主塔的并列布置是必须的氧或氮泵之外不需要工艺泵用于液体输送。在本发明的第一变型中，氩排出塔可以布置在氩排出塔顶部冷凝器的下方。当辅助塔和氩排出塔形成双塔，其中氩排出塔顶部冷凝器为“主冷凝器”时，是优选的。这个双塔然后优选直接位于高压塔的顶部。在高压塔和低压塔一个在另一个布置的情况下，辅助塔、氩排出塔顶部冷凝器和氩排出塔的组合立于或挂在由高压塔和低压塔组成的双塔旁边。
在本发明的第二变型中，氩排出塔和氩排出塔顶部冷凝器在空间上彼此分开布置；特别是氩排出塔布置在低压塔的分隔壁塔区域中。氩排出塔顶部冷凝器和辅助塔的组合仍然位于低压塔的外面，特别是高压塔上方。
高压塔和低压塔优选具有相同的塔直径。“相同的”在本文中被理解为意指小于0.4m的偏差。这允许最佳地利用预定的最大直径。
高压塔(1)，低压塔(2)和辅助塔(14)可以例如具有大于3.5m，特别是大于4.1m的直径。本发明的高压塔、低压塔和辅助塔优选具有大于3.5m，特别是大于4.1m的直径。当辅助塔中的传质元件由具有与低压塔相同或更大的比表面积的规整填料形成时，是有利的。例如，当使用500和750m2/m3的低压塔填料时，辅助塔中的填充密度为例如750或高达1200m2/m3。
此外，有利的是，不将从辅助塔的传质区域流出的全部液体引入到氩排出塔顶部冷凝器的蒸发空间中，而是提供杯状物或其它装置用于捕获就在塔底部上方的辅助塔中向下流的至少部分液体，与用于将收集的液体引入低压塔中的装置相连。
代替在辅助塔的底部布置氩排出塔顶部冷凝器，可以将辅助塔和氩排出塔顶部冷凝器分别布置在不同的容器中。这样可以使得设备部件的布置有更大的灵活性。
特别地，设备部件的两个组合可以并排布置，即高压塔上，特别是主冷凝器上的氩排出塔，和低压塔上的辅助塔。同样有利的是，高压塔和低压塔并排布置，氩排出塔布置在低压塔的上方，辅助塔邻近低压塔和氩排出塔的组合旁边，并且在高压塔之上，特别是在主冷凝器之上。这导致了特别节省空间的装置，这从运输的角度来看是有利的。
附图说明
下面参照附图中以示意图形式描述的两个示例性的实施方案更具体地阐述了本发明以及本发明的进一步细节。附图仅描述了最重要的元件，特别是将本发明的系统与常规空气分离系统区分开的那些元件。
图1示出了根据本发明的第一变型的设备的第一示例性的实施方案，其在高压塔上方具有由辅助塔和氩排出塔组成的双塔，
图2示出了根据本发明的第二变型的第二示例性的实施方案，其中氩排出塔布置在低压塔的分隔壁塔区域中，
图3示出了类似于图1的第三示例性实施方案，但是高压塔和低压塔是一个在另一个上的布置，
图4示出了具有较短辅助塔的图3的修正，
图5示出了补充有氧塔的图3的示例性实施方案，
图6示出了在低压塔上具有辅助塔的另一示例性的实施方案，
图7示出了在高压塔和主冷凝器上具有辅助塔的变型，以及
图8示出了类似于图2的系统，但是具有布置在低压塔中的氩冷凝器。
空气压缩装置、空气净化装置和主热交换器未在附图中示出。也简化了在其它方面的表述；没有标记与理解本发明无关的一些流。
具体实施方式
图1中示例性实施方案的设备包括高压塔1、低压塔2和主冷凝器3。
主冷凝器3在此被配置为多级浴式蒸发器，更具体地为级联式蒸发器。高压塔1和低压塔2并排布置；特别是它们的下端位于相同的测量水平。
进料空气的第一分流4以气体形式流入就在塔底部上方的高压塔1。进料空气的第二部分5至少部分是液体，并且在中间点供应到高压塔1。液体空气的至少一部分通过管道6再次被立即排出，在逆流过冷器7中冷却，并且经由管道108和108b至少部分地在第一中间点供应至低压塔2。
在主冷凝器3中，来自高压塔1的气体顶部氮9的一部分10至少部分地冷凝。由此获得的液氮11的第一部分12作为回流施加到高压塔1的顶部。第二部分13被供应到内部压缩装置(未示出)，最后得到气态压缩氮产物。气体顶部氮9的另一部分14在主热交换器(未示出)中加热，并直接获得为气态压缩产物。
来自高压塔1的液态粗氧15在逆流过冷器7中冷却，并且经管道16和18通过氩排出塔顶部冷凝器17在位于第一中间点下方的第二中间点供应到低压塔2。
从高压塔1上的中间点排出液体不纯氮35，在逆流过冷器中冷却，并通过管道36/136a施加到低压塔2的顶部。其一部分可通过管道37获得，作为液氮产物(LIN)。从低压塔2的顶部排出气态不纯氮气138a，并且在逆流过冷器7中加热之后通过管道39送到主热交换器(未示出)。
使用泵21输送来自低压塔2底部的液氧20的第一部分22到主冷凝器3的蒸发空间中并在那至少部分蒸发。如此形成的气体23被再循环到低压塔2的底部并在那里用作上升气体。液氧20的第二部分24在逆流过冷器7中冷却，并通过管道25作为液氧产物(LOX)排出。液氧20的第三部分26被供给到内部压缩装置(未示出)，最后获得气态压缩氧气产物，为设备的主要产物。
氩排出塔31通常通过气体进料32和液体返回管道33连接到低压塔2上的中间点。在氩排出塔顶部冷凝器17的液化空间中产生用于氩排出塔的液体回流。气体残留产物34从液化空间中排出并在主热交换器中加热。
辅助塔140位于与氩排出塔顶部冷凝器17相同的容器中，其用作辅助塔的底部加热装置，并产生其上升蒸气。自高压塔1的过冷不纯液氮36的一部分136b被用作辅助塔140顶部的回流液体。
过冷液体空气108的一部分108a可以在“第二中间点”供应到辅助塔140。另一部分108b连同涡轮减压空气141的流141一起在相同的中间点或更高位置(未示出)供应到低压塔2。
从辅助塔140的顶部排出气体不纯氮138b，并与低压塔2顶部的气态不纯氮138a混合。在逆流过冷器7中加热后，整个流38经由管道39送至主热交换器(未显示)。或者，两个氮气流138a，138b也可分别输送至，并通过主热交换器。
在辅助塔140的帮助下，降低了低压塔的顶部负荷。因此，所述部分可以被配置成具有较低的容量；相反地，对于相同尺寸的低压塔，整个设备的容量可以增加。
在该示例性的实施方案中，辅助塔和低压塔之间的塔顶压力差为50-150mbar。从图1中的图示出发，来自低压塔2和辅助塔140的顶部馏分138a，138b可以在略微不同的压力下排出，通过逆流过冷器7并供给至主热交换器(未示出))。这也适用于以下示例性的实施方案。
图2中示例性的实施方案与图1中的不同之处在于，氩排出塔17没有布置在氩排出塔顶部冷凝器17的下方，而是布置在低压塔2的分隔壁部分A2中。等效元件在全部附图中具有相同的参考标记。
图2描述了低压塔2的三个部分：下部分A1，中间部分A2和上部分A3。
低压塔2的中间部分A2被配置为分隔壁部分。垂直分隔壁27将第一子空间28和第二子空间29彼此分开。在该实施例中，通过两侧焊接到塔壁的平板金属板形成分隔壁。两个子空间都包含传质单元，例如规整填料。子空间中的传质层可以但不需要具有相同的高度。两个子空间可以具有相同的或不同的尺寸。
第一子空间28形成低压塔1的氩气部分。它与底部的下部分和顶部的上部分流体连通。因此，气体的第一部分可以从下部分通过第一子空间28流到上部分A3。相反地，液体从上部分A3经由第一子空间28流入下部分A1。
第二子空间29形成氩排出塔31。所述子空间同样地与下部分A1流体连通，因此从第一部分A1上升的气体的第二部分可以从那里流入。然而，所述子空间相对于具有水平壁30的上部分A3气密密封。水平壁具有大约半圆形的构造并且焊接到塔壁和分隔壁27。气体既不能从氩排出塔31的顶部流入上部分A3，也不会有液体从那渗透到氩排出塔31中。
在氩排出塔31的顶部，排出富氩气体32，并在氩排出塔顶部冷凝器17的液化空间中部分液化。由此产生的液体33作为回流循环到氩排出塔31中。以气态形式残余的部分以气态形式从氩排出塔顶部冷凝器17中排出成为富氩产物或残余气体34，并经主热交换器(未示出)通过单独的通道组。
由于将氩排出塔31整合到低压塔2中，并且由于在高压塔1上布置氩排出塔顶部冷凝器，与纯氮-氧分离相比，氩排放不需要额外的布置面积。因此可以实现氧产量的增加，而不用设备的明显扩大。
此外，图2中示例性的实施方案包括辅助塔140中的杯状物150和管道151。辅助塔140中向下流的液体完全地，部分地或没有收集在氩排出塔顶部冷凝器上方的杯状物150中。收集的液体经由管道151部分地或完全地引入低压塔2，优选在管道18的上方的低压塔2。这避免了该液体与来自高压塔1的液态粗氧16/氩排出塔顶部冷凝器17的蒸发空间的未蒸发液体的混合。对氩排出塔顶部冷凝器有利的控制也是可能的。
杯状物150和管道151也可以用在所有其它示例性的实施方案中。可以使用任何其它用于液体的收集设备代替杯状物。例如，液体可以收集在烟囱塔盘中或从精馏塔或其降液管中排出。
在图3中，高压塔1，主冷凝器3和低压塔2以常规双塔的形式一个在另一个之上地布置。辅助塔140，氩排出塔顶部冷凝器17和氩排出塔31同样地形成双塔，与图1类似。然而，所述塔没有布置在高压塔1上方，而是紧邻由高压塔1和低压塔2组成的双塔，例如在脚手架上。
此外，并不是全部的粗氧16从高压塔1的底部进入氩排出塔顶部冷凝器的蒸发空间，而是仅仅是一部分经管道16b进入。另一部分经管道16a直接进入低压塔2，其余部分经管道16c传递到辅助塔140上的“第一中间点”。
在图4中，辅助塔140比图3中的稍短，在此由液态空气108形成顶部回流。这通过“回流液管道”408b施加到辅助塔140的顶部。
在图5中，氩排出塔与图3中的相比，有效地向下延伸。氧塔336以额外蒸馏部分的形式位于与氩排出塔31相同的容器中。氧塔336的下端经由气体管道332和液体管道333与紧邻其底部上方的低压塔2连通。
氧塔336的顶部从管道33接收回流液体和/或经由从氩排出塔31流出的液体的至少一部分。氧塔36的容量可以通过两个管道32,33调节。如果液体管道33关闭(或被省略)，则容量精确地分布在两塔之间，使得氧塔336的转化率等于氩排出塔31的转化率。如果更多的容量要转移到氧塔336中，以与图1中标记的流动方向相反的方向将液体经由液体管道33从低压塔2输送到氧塔36中。这个额外的容量从氩排出塔31下方的氧塔336排出并以相应的气体量供给低压塔2。
图5还用虚线描绘了两个旁路管道501，502，其使得可以关闭氩排出塔顶部冷凝器17并继续操作设备的其余部分。然后，管道501将来自氩排出塔顶部冷凝器17的浴的液体通入到氩排出塔31的顶部。通过管道502，来自氩排出塔31的顶部流逆流进入辅助塔140。该特征可以与所有其它示例性的实施方案组合。
图6所示的设备包括用于大气(AIR)的入口过滤器302，主空气压缩机303，空气预冷单元304和空气净化单元305(通常由一对分子筛吸附器形成)，三级、中间冷却以及后冷却的增压空气压缩机306(BAC)和主热交换器308。进料空气的第一子流4以气态形式流入紧邻塔底部上方的高压塔1中。进料空气的第二部分5至少部分是液体，并且在中间点供应到高压塔1。液体空气的至少一部分通过管道6立即再次排出，在逆流过冷器7中冷却，并且经由管道108和108b至少部分地在第一中间点供应至低压塔2。
在主冷凝器3中，来自高压塔1的气体顶部氮9的一部分10至少部分冷凝。由此获得的液氮11的第一部分12作为回流施加到高压塔1的顶部。第二部分13供应到内部压缩装置(泵313)，最后获得气态压缩氮产物。气体顶部氮9的另一部分14被内部压缩(泵621)，在主热交换器308中加热并直接获得气态压缩产物(GANIC)。
来自高压塔1的液态粗氧15在逆流过冷器7中冷却，经管道16传送，然后经过管道18a，18b，18c，在位于第一中间点下方的第二中间点处提供的氩排出塔顶部冷凝器17，低压塔2和辅助塔140之间分配。
在高压塔1上的中间点排出液体不纯氮35，在逆流过冷器中冷却，并经管道36和136a/136b施加到辅助塔140顶部的低压塔2的顶部。气态不纯氮138a的第一流在逆流过冷器7中加热之后经管道39从低压塔2的顶部排出。在加热主热交换器(308)之后，该流被吹送到大气中(ATM)。
使用泵21将来自低压塔2底部的液氧20的第一部分22输送到主冷凝器3的蒸发空间中，并在那里至少部分蒸发。如此形成的气体23再循环到低压塔2的底部并在那用作上升气体。液氧20的第二部分24在逆流过冷器7中冷却，并经管道25排出得到液氧产物(LOX)。内部压缩液氧20的第三部分26，即通过泵321达到期望的产物压力，在主热交换器308中加热的，并最终获得作为设备主要产物的气态加压氧产物(EOXIC)。
氩排出塔31通常通过气体进料32和液体返回管道33连接到低压塔2上的中间点。在氩排出塔顶部冷凝器17的液化空间中产生用于氩排出塔的液体回流。从液化空间排出气体残留产物34,334，在主热交换器308中加热，最后释放到大气中(ATM)；也可以获得富氩产物。
辅助塔140和氩排出塔顶部冷凝器17位于不同的容器中。然而，气体管道61确保-如在前的示例性的实施方案中-在氩排出塔顶部冷凝器17的蒸发空间中产生的气体继续通入到辅助塔140的底部，并且可以作为上升蒸汽。在辅助塔140的底部产生的液体经由液体管道62在合适的中间点供应到低压塔2。来自高压塔1的过冷液体不纯氮36的一部分136b被用作辅助塔140顶部的回流液体。
可以在中间点供应过冷液态空气108的一部分108a到辅助塔140。从辅助塔140的顶部，在比流138a略高的压力下排出气态不纯氮138b的第二流，并在逆流过冷器7和主热交换器308中与第一流138a分开加热，并经过管道638至少部分地/至少间歇地用作空气净化单元305中的再生气体。
在所有示例性的实施方案中，低压塔和氩排出塔之间的气体管道32和液体管道33也可以组合成具有特别大横截面的单个管道。此外，低压塔可以由额外的氮部分补充，其中所述氮部分接收来自高压塔或主冷凝器的专用回流，优选液氮。或者，当辅助塔接受来自高压塔的较纯部分的回流时，辅助塔也可以产生比低压塔更纯的氮。此外，单个元件，多个元件或所有元件，例如空气压缩，空气预冷，空气净化，主热交换器和涡轮机的互连以及来自图6的不纯氮产物的管理可以各自与其它示例性的实施方案组合。
在工艺工程方面，图7很大程度上对应于图6，不过氩排出塔31和辅助塔140在这里互换。辅助塔位于高压塔1和主冷凝器3的上方，氩排出塔31布置在低压塔2的上方。此外，这里还提供了氮压缩器777，以进一步提高气体氮14，714的产物相对于高压塔压力的压力。
图8示出了类似于图3的系统。特别地，低压塔2包含分隔壁部分253。与图2相比，氩冷凝器17结合在低压塔中，没有被构造为简单的浴式蒸发器，而是双层口袋蒸发器(也称为级联式蒸发器)。辅助塔140的底部经由气体管道237和液体管道238与氩冷凝器17的蒸发空间流体连通。从图8中的图示表示，来自低压塔2和辅助塔140的顶部馏分138a，138b在稍微不同的压力下排出，分别通过逆流过冷器7并分别提供给主热交换器(未示出)。

Claims (19)

1.在蒸馏塔系统中通过低温分离空气来制备氧的方法，所述蒸馏塔系统包括：
-高压塔(1)和低压塔(2)，
-主冷凝器(3)，其构造为冷凝器蒸发器，其中所述主冷凝器(3)的液化空间与所述高压塔(1)的顶部流体连通(9,10,11,12)，以及所述主冷凝器(3)的蒸发空间与所述低压塔(2)流体连通，
-与所述低压塔(2)上的中间点(A1/A2)流体连通的氩排出塔(31)，
-氩排出塔顶部冷凝器(17)，其构造为冷凝器-蒸发器，其中所述氩排出塔顶冷凝器(17)的液化空间与所述氩排出塔(31)的顶部流体连通，
-辅助塔(140)，其底部区域构造成用于从所述氩排出塔顶部冷凝器(17)的蒸发空间通入气体，
其中，
-来自所述高压塔(1)底部的液态粗氧(15,16)被引入至所述辅助塔(140)中，
-来自所述高压塔(1)或主冷凝器(3)的液体流经过回流液管道(136b，408a)作为回流引入到所述辅助塔(140)的顶部，其中所述液体流具有至少与空气相等的氮含量，
其特征在于，
-液态粗氧(15,16)的至少第一部分在第一中间点被供应到所述辅助塔(140)，
-在顶部，所述辅助塔(140)在比所述低压塔(2)顶部的操作压力高至少50mbar的压力下操作。
2.根据权利要求1所述的方法，其特征在于，与来自所述低压塔(2)的气体顶部氮(138a)独立地，从所述辅助塔(140)获得气体顶部馏分(138b)作为气体氮产物。
3.根据权利要求1或2所述的方法，其特征在于，额外的液体馏分(108a) 在第二中间点处引入所述辅助塔(140)中，所述第二中间点位于所述第一中间点之上。
4.根据权利要求3所述的方法，其特征在于，所述液体馏分(108a)包括液态空气馏分。
5.根据权利要求1或2所述的方法，其特征在于，在所述辅助塔(140)中向下流的液体的至少一部分在紧邻所述辅助塔底部的上方被收集，并且将至少部分所收集的液体(151)引入所述低压塔(2)中。
6.根据权利要求1或2所述的方法，其特征在于，没有气流从所述低压塔(2)进入所述辅助塔(140)。
7.根据权利要求1或2所述的方法，其特征在于，没有气流并且没有液体流从所述低压塔(2)进入所述辅助塔(140)。
8.根据权利要求1或2所述的方法，其特征在于，所述液态粗氧(15,16)的第二部分供应到所述辅助塔(140)的底部或供应到氩 排出塔顶部冷凝器 (17)的蒸发空间，并且，所述液态粗氧(15,16)的第三部分(16a)在中间点供应到所述低压塔(2)。
9.一种通过低温分离空气制备氧的设备，其具有：
-高压塔(1)和低压塔(2)，
-主冷凝器(3)，其构造为冷凝器蒸发器，其中所述主冷凝器(3)的液化空间与所述高压塔(1)的顶部流体连通(9,10,11,12)，以及所述主冷凝器(3)的蒸发空间与所述低压塔(2)流体连通，
-与所述低压塔(2)上的中间点(A1/A2)流体连通的氩排出塔(31)，
-氩排出塔顶部冷凝器(17)，其配置为冷凝器-蒸发器，其中所述氩排出塔顶部冷凝器(17)的液化空间与所述氩排出塔(31)的顶部流体连通，
-辅助塔(140)，其底部区域被构造成用于从所述氩排出塔顶部冷凝器(17)的蒸发空间经由以下管道通入气体：
-粗氧管道(15,16)，其用于将液态粗氧从所述高压塔(1)的底部引入所述辅助塔(140)中，
-回流液管道(136b，408a)，其用于将来自所述高压塔(1)或所述主冷凝器(3)的液体流作为回流引入所述辅助塔(140)的顶部，其中所述液体流具有至少与空气相等的氮含量，
其特征在于，
-所述粗氧管道(15,16)被配置为用于将所述粗氧在第一中间点引入所述辅助塔(140)，以及其中
-所述辅助塔(140)被配置为用于在比所述低压塔(2)顶部的压力高至少50mbar的辅助塔顶部压力下操作。
10.根据权利要求9所述的设备，其特征在于用于与来自所述低压塔(2)的气体顶部氮(138a)独立地从所述辅助塔(140)获得气体顶部馏分(138b)作为气体氮产物的装置。
11.根据权利要求9或10所述的设备，其特征在于用于将额外的液体馏分(108a)在第二中间点处引入所述辅助塔(140)的中间进料，其中所述第二中间点布置在所述第一中间点之上。
12.根据权利要求9或10所述的设备，其特征在于，所述高压塔和所述低压塔并排布置，并且所述氩排出塔顶部冷凝器(17)和所述辅助塔(140)布置在所述高压塔之上。
13.根据权利要求9或10所述的设备，其特征在于，所述氩排出塔(31)和所述氩排出塔顶部冷凝器(17)在空间上彼此分开布置。
14.根据权利要求9或10所述的设备，其特征在于，所述氩排出塔(31)布置在所述低压塔(2)的分隔壁塔区域(A2)中。
15.根据权利要求9或10所述的设备，其特征在于，所述辅助塔(140)中的传质单元具有与所述低压塔(2)中的传质单元相同或比之更高的比表面积。
16.根据权利要求9或10所述的设备，其特征在于用于在紧邻所述辅助塔底部上方收集所述辅助塔(140)中向下流的液体的至少一部分的装置(150)以及用于将所收集的液体引入到所述低压塔(2)中的装置(151)。
17.根据权利要求9或10所述的设备，其中所述辅助塔(140)和所述氩排出塔顶部冷凝器(17)布置在不同的容器中。
18.根据权利要求16所述的设备，其中所述高压塔(1)和所述低压塔(2)并排布置，所述氩排出塔(31)布置在所述低压塔(2)之上，以及所述辅助塔(140)布置在紧邻所述低压塔(2)和所述氩排出塔(31)的组合并且在所述高压塔(1)的上方。
19.根据权利要求18所述的设备，其中所述辅助塔(140)布置在所述主冷凝器(3)的上方。
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