CN103842753A - 用于通过低温蒸馏分离空气的方法和设备 - Google Patents

用于通过低温蒸馏分离空气的方法和设备 Download PDF

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CN103842753A
CN103842753A CN201280027982.2A CN201280027982A CN103842753A CN 103842753 A CN103842753 A CN 103842753A CN 201280027982 A CN201280027982 A CN 201280027982A CN 103842753 A CN103842753 A CN 103842753A
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tower
oxygen
delivered
pressure column
tower reactor
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CN103842753B (zh
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B·达维迪安
R·杜贝蒂尔-格勒尼耶
L·乔利
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种用于通过低温蒸馏在分离单元中分离空气的方法，所述分离单元包括：热连接在一起的中压塔（23）和低压塔（25），其中富氧液体的流被送至包括塔釜再沸器（61）的纯氧塔的顶部，在该塔釜再沸器中所述流被净化以形成含有至少98mol%氧的塔釜液体并且塔釜液体被抽出作为产品；处于大于第一压力的第二压力下的增压空气流被送至纯氧塔的塔釜再沸器以及被送至液氧蒸发器（51）；富氮气体被从中压塔的顶部抽出；所述气体被送至低压塔的中间再沸器并且冷凝气体被送至中压塔的顶部；富氮气体或空气被送至低压塔的塔釜再沸器（36）并且在该塔釜再沸器中冷凝的液体被送至中压塔。

Description

用于通过低温蒸馏分离空气的方法和设备
本发明涉及通过低温蒸馏分离空气的方法和设备。
本发明尤其提出利用具有双蒸发器的空气分离单元生产纯氧的方法。
根据本发明的方法允许在生产处于低压下的不纯气态氧（小于97mol%或甚至小于96mol%的氧）的设备上、例如在用于富氧燃烧的设备的范围内生产纯液氧（含有至少99mol%或甚至至少99.6mol%的氧）。
生产意在用于氧-煤电厂的氧的空气分离单元（ASU）大致包括位于中压塔（MP塔）和低压塔（LP塔）之间的两个蒸发器（或甚至三个）。安装这两个蒸发器使得可以将MP塔的压力降低到约3bar绝对压力的值，这使得可以将ASU的能量消耗减至最小。
由这种类型电厂生产的氧的纯度通常在95mol%O2和97mol%O2之间。氧的蒸发在专用蒸发器中执行。液态氧的蒸发冷量用于使气态空气冷凝。这种方法通过专利文献US-A-4936099和EP-A-0547946得知。
此外，人们可以尝试利用安装这类ASU以生产纯液氮和纯氧（约99.6%的纯度），储存并随后藉由卡车用于液体贸易。
液氮的生产没有引起任何主要困难，因为足以在MP塔的顶部添加塔板以达到希望的纯度而不影响ASU工艺的其余部分，除了液化能量的成本之外。
然而，纯氧（>99.6%）的生产引起了对方法的更显著的影响；实际上，所生产的液体的纯度明显优于被供应至富氧燃烧电厂的气态氧的浓度。因此有必要安装小的额外的塔，其回收在LP塔中（在塔釜（cuve）中或在中间塔板上）收集的液流的一小部分，蒸馏该小部分，这使得可以在这个小的额外的塔的底部回收意在用于通过卡车交易的纯氧。从纯LOX塔的气态回流然后在与LP塔中的液体的抽取相同的高度处实现。
然而，MP塔的压力很低以至于不可能使用进入或离开MP塔或LP塔待在纯的额外LOX的塔的塔釜蒸发器（其冷凝温度过低）中冷凝的气态流中的一者。
本发明建议使用离开交换管线的气态空气的一小部分作为冷凝流体并且其将随后进入提供纯氧产品的蒸发的专用交换器（以术语HP空气表示）。这个空气流在主交换管线上游被所述单元的主增压器（BAC）压缩。
这股流的压力约为4.5bar abs，大于MP塔的压力，并且因此其始沸点大于纯液氧的平衡温度。
所考虑的空气流和纯氧之间的温差是约2-3℃，此为相对高的值，其使得可以安装小尺寸蒸发器。
在本发明中，根据图1中的替代方案，纯液氧的生产在分离能量方面是免费的并且不影响用于不纯气态氧的生产的分离能量。仅需要支付液化能量。冷量供应可以由独立于ASU的液化系统实现。
本发明建议一种使得可以在具有双蒸发器的空气分离单元上生产纯氧（纯度>99.6%）——通常用于富氧燃烧——的方法，所述纯氧的大部分以约95-97%的纯度被生产。
实际上，利用这种方法，除了HP空气，没有处于足够高以实现纯氧塔的再沸的冷凝温度下的流体可用。
当前，没有用于在具有双蒸发器的空气分离单元上生产纯氧的参考解决方案。
为此，可以使用在主交换管线中的中间高度处（且因此在较高温度下）抽取的流，但是这会使方法复杂。这还会因为必须使用显热而非潜热而不太有效。
可以经常发现具有单一蒸发器的空气分离单元（ASU），其中生产超纯氧的小塔被添加到LP塔的塔釜中。这种情况下，MP塔的压力是约5-6bar，并且超纯LOX塔的再沸通过供给MP塔的气态空气流的一小部分执行。
EP-A-0793069描述了一种根据权利要求1前序部分描述的方法。根据这个方法，处于第一压力下的空气被用于蒸发在蒸发器中的氧，处于高于第一压力的第二压力下的空气被用于使纯氧塔再沸。
US-A-5916262描述了一种利用在塔釜中被空气加热的氧净化塔来生产具有两种纯度的氧的方法。已经被泵加压的液氧也在主交换管路中藉由与增压空气热交换而蒸发。
本发明提出通过安装额外的纯氧塔利用双蒸发器系统生产纯氧，所述纯氧塔的压力等于LP塔的压力。
根据本发明的目的，提供一种用于通过低温蒸馏在分离单元中分离空气的方法，所述分离单元包括：热连接在一起的中压塔和低压塔，其中所述低压塔包括塔釜/塔底再沸器和中间再沸器；以及纯氧塔，其中
i）被净化且然后在交换管线中冷却的处于第一压力下的气态空气被送至所述中压塔，
ii）富氧液体和富氮液体从所述中压塔被送至所述低压塔，
iii）富氮气体被从所述低压塔中抽出，
iv）含有至多97mol%氧的富氧液体被从所述低压塔的塔釜抽出，
v）第一富氧液体流被送至蒸发器并且形成的气态氧被送至交换管线，
vi）第二富氧液体流被送至包括塔釜再沸器的纯氧塔的顶部，该第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体，
vii）处于大于所述第一压力的第二压力下的增压空气流被送至所述纯氧塔的塔釜再沸器，
viii）富氮气体被从所述中压塔的顶部抽出并且被送至所述低压塔的中间再沸器并且冷凝气体被送至所述中间塔的顶部，以及
ix）富氮气体或空气被送至所述低压塔的塔釜再沸器并且在该塔釜再沸器中冷凝得到的液体被送至所述中压塔，
其特征在于，塔釜液体被从所述纯氧塔中作为产品抽出，处于所述第二压力下的增压空气被送至所述蒸发器以使第一富氧液体流蒸发。
根据本发明的其它可选方面：
-第一富氧液体流在蒸发器的上游被加压。
-第一富氧液体流和第二富氧液体流具有相同的纯度。
-处于第二压力下的增压空气被分成两部分，处于第二压力下的增压空气的第一部分被送至纯氧塔的塔釜再沸器，处于第二压力下的增压空气的第二部分被送至蒸发器。
-处于第一压力下的空气被送至低压塔的塔釜再沸器以加热该塔釜再沸器。
-全部空气在交换管线的上游被分成处于第一压力下的流和处于第二压力下的流。
-第一富氧液体流的氧含量少于第二富氧液体流。
-第一富氧液体流在蒸发器中部分地蒸发，其中所形成的液体构成第二富氧液体流。
-处于第二压力下的增压空气流首先加热纯氧塔的塔釜再沸器，然后加热蒸发器。
-处于第一压力下的空气在交换管线中被冷却并且以气态形式被送至中压塔。
-来自辅助源的低温液体被送至双塔。
术语“中压”和“低压”仅表示中压塔在一大于低压塔的压力的压力下运行。这些术语在本领域中常见并且对于本领域技术人员而言是清楚的。
根据本发明的另一目的，提供一种通过低温蒸馏分离空气的设备，所述设备包括：热连接在一起的中压塔和低压塔，其中所述低压塔包括塔釜再沸器和中间再沸器；纯氧塔；交换管线；蒸发器；用于将被净化然后被冷却的处于第一压力下的气态空气从所述交换管线送至所述中压塔的装置；用于将富氧液体和富氮液体从所述中压塔送至所述低压塔的装置；用于将富氮气体从所述低压塔抽出的装置；用于将含有至多97mol%氧的富氧液体从所述低压塔的塔釜抽出的装置；用于将第一富氧液体流送至所述蒸发器的装置；用于将形成的气态氧送至所述交换管线的管道；用于将第二富氧液体流送至包括塔釜再沸器的所述纯氧塔的顶部的装置，所述第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体；增压器；用于将处于大于所述第一压力的第二压力下的增压空气流送至所述纯氧塔的塔釜再沸器的管道；用于将富氮气体从所述中压塔的顶部抽出用以将该富氮气体送至所述低压塔的中间再沸器以及用于将冷凝气体送至所述中压塔的顶部的管道；和用于将富氮气体或空气送至所述低压塔的塔釜再沸器以及用于将在该塔釜再沸器中冷凝的液体送至所述中压塔的管道；其特征在于，所述设备包括用于将塔釜液体从所述纯氧塔作为产品抽出的管道以及用于将处于第二压力下的增压空气从所述增压器送至所述蒸发器的装置。
根据本发明的另外的可选目的，可设想所述设备包括：
-用于将液体从蒸发器送至纯氧塔的顶部的管道，和/或
-用于将塔釜液体从低压塔送至纯氧塔的顶部的管道。
-用于将增压空气从增压器送至蒸发器的装置以使得旨在用于所述蒸发器的空气通过纯氧塔的塔釜再沸器的方式连接至纯氧塔的塔釜再沸器。
-用于将第二富氧液体流送至纯氧塔的顶部的装置包括用于将塔釜液体从低压塔送至纯氧塔的顶部的管道。
-用于将处于第二压力下的增压空气分成两部分的装置，用于将处于第二压力下的增压空气从增压器送至蒸发器的装置以这种方式与用于将处于第二压力下的增压空气流送至纯氧塔的塔釜再沸器的管道连接，即，使得增压空气的一部分被送至纯氧塔的塔釜再沸器且增压空气的另一部分被送至蒸发器。
蒸发器不是蒸馏塔或汽提塔的一部分。
根据本发明的另一目的，提供一种用于通过低温蒸馏在分离单元中分离空气的方法，所述分离单元包括：热连接在一起的中压塔和低压塔，其中所述低压塔包括塔釜再沸器和中间再沸器；以及纯氧塔，其中
i）被净化然后冷却的处于第一压力下的空气被从交换管线送至所述中压塔，
ii）富氧液体和富氮液体从中压塔被送至低压塔，
iii）富氮气体被从低压塔中抽出，
iv）含有至多97mol%氧的富氧液体被从低压塔的塔釜抽出，
v）第一富氧液体流被送至蒸发器并且形成的气态氧被送至交换管线，
vi）第二富氧液体流被送至包括塔釜再沸器的纯氧塔的顶部，该第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体，
vii）处于大于第一压力的第二压力下的增压空气流被送至纯氧塔的塔釜再沸器，
viii）富氮气体被从中压塔的顶部抽出并且被送至低压塔的中间再沸器并且冷凝气体被送至中间塔的顶部，以及
ix）富氮气体或空气被送至低压塔的塔釜再沸器并且在该塔釜再沸器中冷凝的液体被送至中压塔，其特征在于，塔釜液体被从纯氧塔中作为产品抽出，第一富氧液体流的氧含量少于第二富氧液体流。
根据另一些可选特征：
-第一富氧液体流在蒸发器的上游被加压。
-处于第二压力下的第二增压空气流被送至蒸发器。
-第一富氧液体流在蒸发器中部分地蒸发，其中所形成的液体构成第二富氧液体流。
-增压空气流首先加热纯氧塔的塔釜再沸器，然后加热所述蒸发器。
-来自辅助源的低温液体被送至双塔。
-中压塔在2.5bar abs和4.5bar abs之间的压力下运行。
根据本发明的另一目的，提供一种通过低温蒸馏分离空气的设备，所述设备包括：热连接在一起的中压塔和低压塔，其中所述低压塔包括塔釜再沸器和中间再沸器；纯氧塔；交换管线；蒸发器；用于将被净化然后被冷却的处于第一压力下的气态空气从所述交换管线送至所述中压塔的装置；用于将富氧液体和富氮液体从所述中压塔送至所述低压塔的装置；用于将富氮气体从所述低压塔抽出的装置；用于将含有至多97mol%氧的富氧液体从所述低压塔的塔釜抽出的装置；用于将第一富氧液体流送至所述蒸发器的装置；用于将形成的气态氧送至所述交换管线的管道；用于将第二富氧液体流送至包括塔釜再沸器的所述纯氧塔的顶部的装置，所述第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体；增压器；用于将处于大于所述第一压力的第二压力下的增压空气送至所述纯氧塔的塔釜再沸器的管道；用于将富氮气体从所述中压塔的顶部抽出以便将该富氮气体送至所述低压塔的中间再沸器以及用于将冷凝气体送至所述中压塔的顶部的管道；和用于将富氮气体或空气送至所述低压塔的塔釜再沸器以及用于将在该塔釜再沸器中冷凝得到的液体送至所述中压塔的管道；其特征在于，所述设备包括用于将塔釜液体从所述纯氧塔作为产品抽出的管道以及用于将液体（53）从所述蒸发器（51）送至所述纯氧塔（49）的顶部的管道。
所述设备还可以包括用于将塔釜液体从所述低压塔送至纯氧塔的顶部的管道。
用于将增压空气从增压器送至蒸发器的装置可以使得旨在用于蒸发器的空气通过纯氧塔的塔釜再沸器的方式连接至纯氧塔的塔釜再沸器。
用于将第二富氧液体流送至纯氧塔的顶部的装置可以包括用于将塔釜液体从低压塔送至纯氧塔的顶部的管道。
所述设备可以包括用于将处于第二压力下的增压空气分成两部分的装置，其中用于将处于第二压力下的增压空气从增压器送至蒸发器的装置以这种方式与用于将处于第二压力下的增压空气流送至纯氧塔的塔釜再沸器的管道连接，即，使得增压空气的一部分被送至纯氧塔的塔釜再沸器且增压空气的另一部分被送至蒸发器。
所述设备可以包括用于将低温液体从外部源送至低压塔的装置。
所述设备可以包括用于将增压空气流从纯氧塔的塔釜再沸器送至蒸发器的管道，以及用于将空气从蒸发器送至中压塔和/或低压塔的管道。
根据另一替代方案，所述设备包括用于将增压空气流从纯氧塔的塔釜再沸器直接送至中压塔和/或低压塔的管道。
本文描述的本发明的主要创新特征是纯氧塔的再沸是通过离开主交换管线的气态空气流（HP空气）的一小部分来实现，该气态空气流被增压器压缩处于在蒸发器中的氧的蒸发所要求的压力下。HP空气的这一小部分在纯氧塔的冷凝器中部分地或完全地冷凝。
根据一替代方案，部分冷凝的增压空气流——可能地在已经分离出冷凝部分（该冷凝部分随后被送至MP塔）以后——被随后送至产品蒸发器，所述增压空气流在该产品蒸发器中彻底完成冷凝。增压空气的部分冷凝使得可以在GOX的生产的实际额定流量和相同压力的情况下运行具有纯塔塔釜的蒸发器以及然后运行产品蒸发器。纯液氧塔的再沸因此关于蒸发产品所要求的能量是免费的。
所述空气流的压力高于MP塔的压力（与3.2bar abs相比通常为约4.5bar abs）。
产品蒸发器中的不纯液体的一部分（在相同高度并代替蒸发器的稀释清洗物）被抽取出并且被送到纯液氧塔中，该纯液氧塔是在与产品蒸发器的压力基本上相同的压力下蒸馏的塔。
来自纯氧塔的不纯气态回流与来自产品蒸发器的气态流混合，这两股流构成不纯GOX的产品的额定流量。
纯液体被从纯氧塔的塔釜中取出。其也被用作用于整个设备的稀释清洗物。
冷量（frigorie，负大卡）的供应可以由独立的液化器例如通过利用（来自尖塔的）纯氮生产液氮来提供，所述纯氮会随后以液体形式被加入设备中。如果不生产液体纯氮，则可以设想在独立的液化器中使残余氮液化。
如果纯液体的产量低，则还可以设想将冷却系统合并到ASU中。
将参考附图更详细地描述本发明，所述附图示出根据本发明的用于分离空气的方法。
在图1中，空气在包括用于分离空气的双塔的ASU中分离，所述双塔包括中压塔23和低压塔25。用于分离的冷量藉由中压氮在涡轮47内的膨胀来提供。设备包括纯液氧塔49、泵57、蒸发器51和交换管线63。
空气1被压缩机3加压而处于在2.5bar abs和4.5bar abs之间的压力下。然后，空气在净化单元5内藉由吸附被净化。净化空气7被分成两个部分。一个部分9在增压器13内升压到在4bar abs和20bar abs之间的压力，然后在交换管线63内冷却直到冷端。空气9被分成两个小部分15、17。一个小部分15被送至蒸发器15，其在该蒸发器中用于部分地蒸发含有最多97mol%氧的液氧用以产生在交换管线63内被加热的气态氧59。这些气体59被送至富氧燃烧单元。富氧液体53从蒸发器51中被抽取作为清洗物。空气被冷凝。空气的另一小部分17被送至纯氧塔49的塔釜再沸器61。这个塔包括塔釜再沸器和用于在该再沸器上方进行热交换和物质交换的装置。包括至多97mol%氧的液氧65被送至塔49的顶部并且被增浓以形成从塔釜中抽取出的且含有至多98mol%氧的液体产品71。来自塔49的顶部的气态氧被送至低压塔25的塔釜。冷凝空气17与来自蒸发器51的冷凝空气混合并且在于阀21内膨胀以后被送至在2.5bar abs和4.5barabs之间的压力下运行的MP塔23。
空气的另一部分11在交换管线63中冷却、被送至LP塔25的塔釜再沸器35、在该塔釜再沸器内至少部分地冷凝并被送至位于液态空气19的进口下方的MP塔23的塔釜。
富氧液体27被从MP塔23的塔釜抽出、在过冷器33内冷却、膨胀并被送至LP塔25。液体29被从MP塔23抽出、在过冷器33内冷却、膨胀并且被送至LP塔25。富氮液体31被从MP塔23的顶部抽出、在过冷器33中冷却、膨胀并且被送至LP塔25的顶部。
低压氮39被从LP塔的顶部抽出、在过冷器33中被加热并且在交换管线63中被加热。
中压氮41被分成两部分以形成部分43和部分45。部分43用于加热低压塔25的中间再沸器37。部分45在交换管线63中被加热、在涡轮47中膨胀并且被送回到交换管线63。液氧被从LP塔的塔釜抽出并被分成两部分。部分55在位于蒸发器51的上游的泵57内被加压，余下部分65在不被加压的情况下被送至纯氧塔49的顶部。纯氧塔49的顶部因此与低压塔25的塔釜处于相同压力下。清洗液体53的全部或一部分也可以供应塔49的顶部。
低温液体流69（例如，液氮）被送至LP塔的顶部以保持该方法处于冷却状态。
图1a中的方法与图1中的方法的区别在于，塔49在其顶部专门由蒸发器51的清洗物53继在阀中的膨胀步骤之后供应。塔49的塔釜再沸器61仍通过增压空气17被加热，其中冷凝空气与被用于加热蒸发器51的增压空气15混合。还可能向该塔供应清洗液体53和来自低压塔25的塔釜的液氧65。
图2中的方法与图1中的方法的区别在于，空气流9首先被送至纯氧塔49的塔釜蒸发器61，然后被送至该空气流在其中冷凝的蒸发器51。所形成的空气在阀21中膨胀并且被送至中压塔23。空气的一小部分11在交换管线11中冷却并且在没有在压缩机3的下游膨胀或压缩的情况下被送至中压塔23的塔釜。
中间再沸器37始终由中压氮43加热，但是中压氮的另一部分73在利用低温温度的冷增压器71中被压缩并且被送至塔釜再沸器35。冷凝氮在阀36中膨胀并且被送至MP塔23的顶部。低压塔的塔釜氧55全部在泵57中被加压并被送至所述氧在其中部分地蒸发的蒸发器51。蒸发气体构成含有少于97mol%氧的气态氧产品59。未蒸发液体53供应塔49的顶部。来自塔49的顶部的气态氧67与气态氧59混合。液氧71构成液体产品。这种情况下，纯氧塔49不与LP塔25在相同的压力下运行。
图1或图1a中的方法可以使用氮加热塔釜再沸器35，图2中的方法可以利用空气加热塔釜再沸器35。

Claims (15)

1.一种用于通过低温蒸馏在分离单元中分离空气的方法，所述分离单元包括：热连接在一起的中压塔（23）和低压塔（25），其中所述低压塔包括塔釜再沸器（35）和中间再沸器（37）；以及纯氧塔（49），其中
i）将被净化且然后在交换管线中冷却的处于第一压力下的气态空气送至所述中压塔，
ii）将富氧液体和富氮液体从所述中压塔送至所述低压塔，
iii）从所述低压塔中抽取富氮气体，
iv）从所述低压塔的塔釜抽取含有至多97mol%氧的富氧液体，
v）将第一富氧液体流送至蒸发器（51）并且将形成的气态氧送至所述交换管线，
vi）将第二富氧液体流送至包括塔釜再沸器（61）的纯氧塔的顶部，该第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体，
vii）将处于大于所述第一压力的第二压力下的增压空气流送至所述纯氧塔的塔釜再沸器，
viii）从所述中压塔的顶部抽取富氮气体并且将其送至所述低压塔的中间再沸器并且将冷凝气体送至所述中压塔的顶部，以及
ix）将富氮气体或空气送至所述低压塔的塔釜再沸器并且将在该塔釜再沸器中冷凝的液体送至所述中压塔，
其特征在于，从所述纯氧塔抽取塔釜液体作为产品，将处于所述第二压力下的增压空气送至所述蒸发器以使所述第一富氧液体流蒸发。
2.根据权利要求1所述的方法，其特征在于，所述第一富氧液体流在所述蒸发器（51）的上游被加压。
3.根据权利要求1或2所述的方法，其特征在于，所述第一富氧液体流和所述第二富氧液体流具有相同的纯度。
4.根据权利要求3所述的方法，其特征在于，所述处于第二压力下的增压空气被分成两部分，所述处于第二压力下的增压空气的第一部分被送至所述纯氧塔的塔釜再沸器，所述处于第二压力下的增压空气的第二部分被送至所述蒸发器（51）。
5.根据权利要求1或2所述的方法，其特征在于，所述第一富氧液体流的氧含量小于所述第二富氧液体流。
6.根据权利要求5所述的方法，其特征在于，所述第一富氧液体流在所述蒸发器（51）中部分地蒸发，其中所形成的液体构成所述第二富氧液体流。
7.根据权利要求6所述的方法，其特征在于，所述处于第二压力下的增压空气流首先加热所述纯氧塔（49）的塔釜再沸器（61），然后加热所述蒸发器（51）。
8.根据前述权利要求中任一项所述的方法，其特征在于，来自辅助源的低温液体（69）被送至双塔。
9.一种通过低温蒸馏分离空气的设备，所述设备包括：热连接在一起的中压塔（23）和低压塔（25），其中所述低压塔包括塔釜再沸器（35）和中间再沸器（37）；纯氧塔（49）；交换管线（63）；蒸发器（51）；用于将被净化然后被冷却的处于第一压力下的气态空气从所述交换管线送至所述中压塔的装置；用于将富氧液体和富氮液体从所述中压塔送至所述低压塔的装置；用于从所述低压塔抽取富氮气体的装置；用于从所述低压塔的塔釜抽取含有至多97mol%氧的富氧液体的装置；用于将第一富氧液体流送至所述蒸发器的装置；用于将形成的气态氧送至所述交换管线的管道；用于将第二富氧液体流送至包括塔釜再沸器（61）的所述纯氧塔的顶部的装置，所述第二富氧液体流在该塔釜再沸器中被净化以形成含有至少98mol%氧的塔釜液体；增压器（3）；用于将处于大于所述第一压力的第二压力下的增压空气流（17）送至所述纯氧塔的塔釜再沸器的管道；用于从所述中压塔的顶部抽取富氮气体以便将该富氮气体送至所述低压塔的中间再沸器以及用于将冷凝气体送至所述中压塔的顶部的管道；和用于将富氮气体或空气送至所述低压塔的塔釜再沸器以及用于将在该塔釜再沸器中冷凝得到的液体送至所述中压塔的管道；其特征在于，所述设备包括用于从所述纯氧塔抽取塔釜液体（71）作为产品的管道以及用于将处于第二压力下的增压空气（15）从所述增压器送至所述蒸发器的装置。
10.根据权利要求9所述的设备，其特征在于，所述设备包括：
i）用于将液体（53）从所述蒸发器（51）送至所述纯氧塔（49）的顶部的管道，和/或
ii）用于将塔釜液体（65）从所述低压塔（25）送至所述纯氧塔（49）的顶部的管道。
11.根据权利要求10所述的设备，其特征在于，用于将增压空气从所述增压器（3）送至所述蒸发器（51）的装置以使得旨在用于所述蒸发器的空气通过所述纯氧塔的塔釜再沸器的方式连接至所述纯氧塔（49）的塔釜再沸器（61）。
12.根据权利要求9或10所述的设备，其特征在于，用于将第二富氧液体流送至所述纯氧塔的顶部的装置包括用于将塔釜液体从所述低压塔（65）送至所述纯氧塔（49）的顶部的管道。
13.根据权利要求9、10或12所述的设备，其特征在于，所述设备包括用于将处于所述第二压力下的增压空气分成两部分的装置，其中用于将处于所述第二压力下的增压空气从所述增压器（3）送至所述蒸发器（51）的装置以这种方式与用于将处于所述第二压力下的增压空气流送至所述纯氧塔（49）的塔釜再沸器（61）的管道连接，即，使得增压空气的一部分（17）被送至所述纯氧塔的塔釜再沸器且增压空气的另一部分（15）被送至所述蒸发器。
14.根据权利要求9-13中任一项所述的设备，其特征在于，所述设备包括用于将液体（53）从所述蒸发器（51）送至所述纯氧塔（49）的顶部的管道，以及用于将塔釜液体（65）从所述低压塔（25）送至所述纯氧塔（49）的顶部的管道。
15.根据权利要求9-14中任一项所述的设备，其特征在于，所述设备包括用于将低温液体从外部源送至低压塔的装置（69）。
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