CN1760612A - 空气的低温蒸馏方法 - Google Patents

空气的低温蒸馏方法 Download PDF

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CN1760612A
CN1760612A CNA200510113618XA CN200510113618A CN1760612A CN 1760612 A CN1760612 A CN 1760612A CN A200510113618X A CNA200510113618X A CN A200510113618XA CN 200510113618 A CN200510113618 A CN 200510113618A CN 1760612 A CN1760612 A CN 1760612A
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P·希格金博塔姆
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Abstract

在一种方法中生产加压气态氮(“GAN”)，该方法中液氮(“LIN”)在低温空气分离单元(“ASU”)124，150中生产。将至少部分LIN的压力提高164以生产加压LIN。在辅助低温蒸馏塔196中将氧浓度至少与空气相同的流体分离，生成富氮塔顶蒸气和浓集氧的塔底液体。在至少部分富氮塔顶蒸气与至少部分加压LIN之间传热和任选地传质166，503以生成富氮液体和加压GAN。在适当的压力调节173之后，将至少部分所述富氮液体作为回流用于ASU。这种方法使得能够生产高纯度GAN而无氧回收损失，这种损失通常在常规泵送式LIN循环中可见。

Description

空气的低温蒸馏方法
本发明涉及一种空气的低温蒸馏方法，特别涉及高纯、加压气态氮(“GAN”)的生产。
高纯GAN通常在进行泵送式液氮(“LIN”)循环的低温空气蒸馏过程中制备。这种循环中，将取自蒸馏***的LIN泵送(pump)至所需的产品压力，并在主换热器中通过与冷凝中的高压空气间接换热而蒸发。将所得液体空气(“LAIR”)供入塔***。然而，当与高压(“HP”)GAN循环相比时，采用这种泵送式LIN循环通常导致不利的氧回收损失，高压GAN循环中将氮以蒸气形式从双塔蒸馏***的HP塔取出，在主换热器中加温并压缩至期望压力。这是因为：在泵送式LIN循环中将伴以氮沸腾而冷凝的部分原料空气在HP塔中预分离成LIN和粗液氧中并不如HPGAN循环中的蒸气空气原料同样高效。从而，双塔***的低压塔(“LP”)必须进行更多的分离，结果总体氧回收下降。
US-A-5419137(Sweeney等，1995年5月30日公开)披露了一种空气分离方法，用双塔蒸馏***生产高纯氮。用冷凝器将LP塔中的塔顶(overhead)蒸气通过与取自HP塔的高纯LIN间接换热而部分冷凝。将所得高纯GAN作为产品移出，但是该产品为低压，因此需要单另的氮气压缩机以将GAN产品压缩至期望的压力。冷凝器位于LP塔的塔顶部分内。这篇参考文献还披露了一种排布方式，其中用与LP塔呈直接传热和传质关系的汽提塔(常常称作顶罩塔)代替冷凝器。
US-A-4433989(Erickson，1984年2月28日公开)披露了一种空气分离方法，采用配有辅助蒸馏塔的双塔***生产GAN。在辅助塔中，将来自HP塔贮槽的粗液氧分离成富氮的塔顶蒸气和浓集氧的塔底液体。将来自HP塔的LIN减压并用作辅助塔的回流。从该塔将塔顶富氮蒸气作为产品取出，不抽取LIN产品。
US-A-4433989还披露了一种更进一步的辅助塔，其中，将空气在该更进一步的辅助塔中分离成富氧的塔底液体和富氮的塔顶蒸气。该更进一步的辅助塔以通过间接换热冷凝的塔顶氮蒸气回流，该间接换热是与取自LP塔通过泵送LOX提供的加压LOX进行。从该更进一步的辅助塔中移出冷凝的塔顶蒸气并作为回流供入HP塔。
US-A-6276171(Brugerolle，2001年8月21日公开)披露了一种集成了空气分离单元(“ASU”)的燃气涡轮。LIN在ASU中制造，泵送并供入氮洗涤塔。将GAN以8-25bar(0.8-2.5MPa)的压力从氮洗涤塔移出、加温、压缩并在实施膨胀前与来自燃气涡轮的燃烧废气混合。塔底液体从洗涤塔移出、膨胀并供入ASU。主要希望将洗涤塔用于生产低纯氮。
US-A-5596886(Howard，1997年1月28日公开)披露了一种空气分离方法，用配有浓集氮的辅助塔的双塔***生产气态氧(“GOX”)和高纯氮。将来自HP塔的富氮塔顶蒸气加温、压缩、冷却，然后供入以LIN回流的辅助塔。将浓集氮的塔顶蒸气从辅助塔移出，通过与来自LP塔的LOX间接换热而冷凝形成LIN。将LIN泵送，并将部分泵送的LIN供入辅助塔顶部。
US-A-4790866(Rathbone，1988年12月13日公开)披露了一种空气分离方法，采用配有氩塔的双塔***。将LIN从HP塔移出并在减压后供入氩塔的冷凝器，在此促进氩塔塔顶蒸气的冷凝。
需要一种方法，该方法能够在不同于该ASU操作压力的压力下生产高纯GAN而不降低氧回收量。
根据本发明的第一方面，提供一种生产加压气态氮(“GAN”)的方法，该方法包含：
在低温空气分离单元(“ASU”)中生产液氮(“LIN”)；
将至少部分所述LIN加压以生产加压的LIN；
在辅助低温蒸馏塔中分离氧气浓度至少与空气相同的流体，以生产富氮的塔顶蒸气和浓集氧的塔底液体；
在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间进行传热和任选的传质，以生产富氮的液体和加压GAN；以及
在适当的压力调节后，将至少部分所述富氮的液体作为回流供给ASU。
措辞“富氮的”是指氮含量比空气中高。措辞“浓集氮的”是指在进行了特定处理步骤后氮含量更高。措辞“富氧的”和“浓集氧的”与如上给出的“富氮的”和“浓集氮的”具有类似的含义。富氮液体的纯度通常比LIN的纯度低，优选有约85mol％氮至约99mol％氮之间的纯度，例如约95mol％氮。
本发明优选的方法使得能够在不同压力下从塔中生产高纯度GAN，在所述塔中通常无氧回收损失地分离高纯度LIN，该氧回收损失通常在传统泵送式LIN循环中可见，该循环中氮沸腾，伴以空气冷凝。
优选的方法所需的分离级数也更少。例如，在富氮塔顶蒸气通过与LIN间接换热使LIN蒸发而冷凝的实施方案中，由于辅助塔无需制造纯LIN，因此仅需要较少的分离级。在LIN与富氮塔顶蒸气之间传热和传质的实施方案中，辅助塔的顶部以高于没有返回ASU的物流时的回流比操作，因而需要较少的分离级就能达到相同的纯度级。
与高纯氮直接在洗涤塔中沸腾的循环相比，该洗涤塔没有低纯氮返回ASU，优选的方法还对操作异常较不敏感。例如，在富氮塔顶蒸气通过与蒸发中的LIN间接换热而冷凝的实施方案中，辅助塔无需制造纯LIN因此仅需在生产LIN的ASU塔中保持纯度。在LIN与富氮塔顶蒸气之间传热和传质的实施方案中，顶部以高于没有返回ASU的物流时的回流比操作，因而纯度对回流比中的操作变动较不敏感。
在优选的实施方案中，还可以扩大氮生产的操作范围(即能够高效地，例如不必排放过量氮气或向辅助塔供入过量空气地，提供的氮生产率的范围)，并且在塔性能劣化的情形中可以更容易地保持氮纯度。
在适当的压力调节后，将富氮液体用作ASU中的回流。在ASU包含双塔蒸馏***之处，通常将富氮液体用作LP塔中的回流。优选地，在适当的压力调节或减压后，还将至少部分浓集氧的液体供入ASU，可能作为回流。在ASU包含双塔蒸馏***之处，通常将至少部分富氧液体直接供入LP塔(尽管可以将它经HP塔供入，以回收在HP塔压力下闪蒸出的任何蒸气)。
流体的氧浓度至少与空气相同。流体可以为空气或来自ASU的富氧流体。流体可以为气态或液态。在流体为液态的方法实施方案中，随后通常用位于辅助塔贮槽中的再沸器/冷凝器将至少部分液体通过与适宜的过程物流间接换热而蒸发。适宜的过程物流包括例如来自LP或HP塔的侧流；或者如果存在，来自氩塔的侧流；或增压空气压缩机侧流所供应的高压空气；再循环的氮流或已在低温下压缩的来自主塔***的空气流或氮流。
LIN的压力可以由静压头来增加。然而，优选将LIN泵送以增加其压力。
富氮塔顶蒸气可以通过与加压的LIN间接或直接换热而冷凝。
热量可以在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间间接交换，由此，将所述富氮塔顶蒸气冷凝生成富氮液体以及将所述加压LIN蒸发生成加压GAN。在这种方法实施方案中，可用再沸器/冷凝器间接交换热量。如果再沸器/冷凝器位于辅助塔内主蒸馏区或段之上，那么加压LIN就可以穿过再沸器/冷凝器，由此将再沸器/冷凝器周围的富氮塔顶蒸气冷凝。如果再沸器/冷凝器位于辅助塔外层，那么富氮塔顶蒸气就可以穿过再沸器/冷凝器，将再沸器/冷凝器周围的加压LIN蒸发。
辅助塔通常包含至少一个主蒸馏区。可以在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间直接传热和传质，生成富氮液体和加压GAN。在这种实施方案中，辅助塔优选具有至少一个主蒸馏区以及位于该主蒸馏区上方的气/液接触促进构件。该方法包含使富氮塔顶蒸气与加压LIN在接触促进构件中直接接触，生成富氮液体和加压GAN。接触促进构件通常是另一蒸馏区(a further distillation zone)。在这另一蒸馏区中，液气比大大高于从主蒸馏区顶部的不纯氮蒸气生产高纯氮所需的最小值。结果，与没有不纯液氮返回的方法相比，可以采用相对较少的蒸馏级。
辅助塔可以以任何适宜的液体回流，例如LAIR。然而，优选将部分富氮液体用于回流入辅助塔。
ASU可以包含任何适宜的蒸馏塔排布，包括生产LIN的单个蒸馏塔。然而，在优选的方法实施方案中，ASU是双塔***，该***包含HP蒸馏塔和LP蒸馏塔，HP塔与LP塔通过ASU再沸器/冷凝器热结合。在这类实施方案中，该方法进一步包含：
在HP塔中将空气分离成HP富氮塔顶蒸气和富氧塔底液体；
在LP塔中将至少部分富氧塔底液体分离成LP富氮塔顶蒸气和LOX；
在所述ASU再沸器/冷凝器中通过与LOX的间接换热将至少部分HP富氮塔顶蒸气冷却并至少部分冷凝，生成所述LIN；以及
以部分所述LIN回流HP塔。
在适当的压力调节后，可将HP塔中生成的部分富氧塔底液体用作至少部分流体。富氧塔底液体可以通过静压头加压，但是优选用泵加压。
在这类方法实施方案中，辅助塔的操作压力通常高于LP塔的操作压力，并且优选高于HP塔的操作压力。就此而言，LP塔的典型操作压力为约1.2巴(0.12MPa)-约4巴(0.4MPa)，HP塔为约4巴(0.4MPa)-约12巴(1.2MPa)。优选的操作压力对HP塔为约4.8巴(0.48MPa)，对LP塔为1.3巴(0.13MPa)。辅助塔的操作压力可以为约1.0巴(0.10MPa)-约30巴(3.0MPa)，通常为约1.5巴(0.15MPa)-约25巴(2.5MPa)。优选地，辅助塔的操作压力为约12巴(1.2MPa)。
加压GAN通常在辅助塔的操作压力下生产，且通常在约1.0巴(0.1MPa)-约25巴(2.5MPa)的压力下生产，并且通常为高纯度，例如约99.9mol％氮-约99.9999mol％氮，典型地约99.99mol％氮。
根据本发明的第二方面，提供生产加压GAN的装置，该装置包含：
包含至少一个蒸馏塔的低温ASU，用于生产LIN；
加压构件，用于将LIN加压；
管件，用于将来自生产所述LIN的ASU塔顶的LIN供给加压构件；
包含主蒸馏区的辅助低温蒸馏塔，用于将氧含量至少与空气相同的流体分离成富氮塔顶蒸气和浓集氧的塔底液体；
能使传递进行的构件，用于能够在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间传热和任选地传质，以生产富氮液体和加压GAN；
管件，用于将来自加压构件的加压LIN供给能使传递进行的构件；
减压构件，用于降低富氮液体的压力以生产减压的富氮液体；
管件，用于将来自辅助塔的富氮液体供给减压构件；以及
管件，用于将来自所述减压构件的减压富氮液体作为回流供给ASU。
能使传递进行的构件可以是冷凝构件，用于通过与加压的LIN间接换热而使至少部分富氮塔顶蒸气冷凝，生成富氮液体和加压GAN。在另一种实施方案中，能使传递进行的构件可以是气/液接触促进构件，例如另一蒸馏区，用于促进富氮塔顶蒸气与加压LIN之间的直接接触，该接触促进构件位于辅助蒸馏塔内主蒸馏区上方。
如上所述，ASU可以包含单个蒸馏塔。但是，在优选的实施方案中，ASU包含双蒸馏塔***。在这种优选的实施方案中，可以将减压的富氮液体或者供给HP塔、或者供给LP塔。还优选在减压之前将其过冷(subcool)以使闪蒸的形成最小化。
该装置优选还包含：减压构件，用于降低浓集氧液体的压力以生产减压浓集氧液体；管件，用于将来自辅助塔的浓集氧液体供给该减压构件；以及管件，用于将来自该减压构件的减压浓集氧液体供给ASU，可以作为回流。如果ASU包含双塔***，那么通常将减压的浓集氧液体供给LP塔，通常通过HP塔的底部。
每种减压构件可以是任何用于降低低温液体或气体压力的适宜构件。然而，优选减压构件为膨胀阀，例如Joule-Thompson阀。
可以调整和/或构造该装置，使得能够实施任何上述优选的方法实施方案。
如上文，结合附图充分描述该方法或装置的特别优选的实施方案。
现将结合附图描述本发明的优选实施方案，其中：
图1是适用于本发明的一种辅助塔的图示；
图2是适用于本发明的另一种辅助塔的图示；
图3是根据本发明方法的一种实施方案的流程图；
图4是根据本发明方法的另一种实施方案的流程图；
图5是根据本发明方法的又一种实施方案的流程图；以及
图6是实施例中由计算机模拟的方法的流程图。
参照图1，将空气或富氧流体(例如用泵(未示出)或者如果原料为蒸气则用压缩机(未示出)加压后的来自双塔ASU(未示出)中HP塔的富氧塔底液体，)的物流12供给辅助蒸馏塔14的底部，在此将其分离成富氮的塔顶蒸气和浓集氧的塔底液体。当流体为液体时，用任选的再沸器/冷凝器16通过与过程物流的间接换热而将至少部分流体蒸发。
从ASU取出纯LIN物流18并在泵20中泵送。将加压LIN的物流22供给位于辅助塔14外部的再沸器/冷凝器24，在此通过与来自辅助塔14的富氮塔顶蒸气的间接换热而蒸发，生成加压GAN的物流26和用作辅助塔14的回流的富氮液体。从辅助塔14取出富氮液体物流28，在适当的压力调节之后，作为回流供给ASU(未示出)。从辅助塔14取出浓集氧塔底液体的物流30，同样在适当的压力调节后，作为回流供给ASU(未示出)。
图2中所示过程与图1中所示的相似，相同的附图标记用于指示在每个图中相同的特征。以下描述仅涉及图2所示与图1中所示特征不同的特征。
图2中，再沸器/冷凝器24已经用辅助塔14中另外的蒸馏区或段32代替。富氮塔顶蒸气在该另外的蒸馏塔段32中与来自物流22的加压LIN进行直接接触。同时传热和传质，生成富氮液体(作为物流28移出)和加压GAN(作为物流26移出)。
现在参照图3，原料空气的物流100在压缩机102中压缩，用净化单元104将水和二氧化碳从所得压缩原料空气流中移出。将净化的压缩原料空气分成三股物流106、108和122。
物流108在主换热器112中通过与产物流间接换热加热产物流而冷却，生成冷却的压缩原料空气的物流110，然后将物流110送至双蒸馏塔***HP塔124的底部。
物流122在压缩机123中进一步压缩，生成进一步压缩的原料空气物流126，然后将其在主换热器112中冷却，生成冷却的进一步压缩的原料空气物流128，然后在适当的压力调节后，将该物流128送到HP塔124的中间位置。进一步压缩的原料空气的第二物流325从压缩机123的中间级移出，在主换热器112中冷却，然后作为物流127送至辅助塔196的塔底。
压缩原料空气的物流106在压缩机115中进一步压缩，将该进一步压缩的原料空气在主换热器112中冷却至其温端与冷端之间的中间温度，由此作为物流116移出并在膨胀器118中膨胀，为该过程提供致冷。将经膨胀的原料空气物流120送至双蒸馏塔***LP塔150的中间位置。
将作为物流110和128供给HP塔124的原料空气分离成HP塔富氧塔底液体和HP塔富氮塔顶蒸气。将作为物流127供给辅助塔196的原料空气分离成辅助塔富氧塔底液体和辅助塔富氮塔顶蒸气。将辅助塔富氧塔底液体的物流167从辅助塔196移出，经阀168减压，与来自HP塔的HP塔富氧塔底液体结合形成富氧塔底液体物流152，将该物流152经阀153送至LP塔150的中间位置。液体物流130从HP塔124的中间位置移出，并在经阀131减压后供给LP塔150。
将HP塔富氮塔顶蒸气的物流158从HP塔124的塔顶移出，在位于LP塔150贮槽内的冷凝器160中通过与LOX间接换热而冷凝，生成LIN物流162。一部分来自物流162的LIN作为回流送至HP塔124的顶部。第二部分以物流170在经阀171减压后作为回流送至LP塔150的顶部。第三部分以物流163供给泵164，在此将其泵送生成加压LIN物流165。
加压物流LIN的物流165在再沸器/冷凝器161中通过与辅助塔富氮塔顶蒸气的物流159间接换热而沸腾，生成加压GAN物流166和富氮液体物流。加压GAN物流166在主换热器112中加温，伴以将原料空气冷却，生成加压GAN产物流168。将部分富氮液体作为回流送至辅助塔196的顶部，并将剩余部分以物流169在经阀173减压后作为回流送至LP塔150的顶部。
将LP塔150的原料物流分离成LP塔顶氮蒸气和LOX。LOX物流180从LP塔150移出，在泵182中加压，生成加压LOX的物流184，将该物流184在主换热器112中加温生成GOX物流186。气态氮的物流172从LP塔150的塔顶移出，在主换热器112中加温生成LPGAN物流176。
图4-6中所示过程与图3中所示的相似，相同的附图标记用于指示在每个图中相同的特征。以下描述仅涉及图4-6所示与图3中所示特征不同的特征。
图4中，辅助塔196不具有再沸器/冷凝器161.相反，该塔具有位于主蒸馏区501之上的进一步蒸馏区503。加压LIN的物流165送至辅助塔196的顶部，将加压GAN的物流166从辅助塔196的顶部移出。将富氮液体的物流169从辅助塔196内的中间位置移出，并在经阀173减压后送至LP塔150的顶部。
图5中所示过程与图4中所示的相似，辅助塔196具有位于主蒸馏段501之上的进一步蒸馏段503。至HP塔124的中间回流由经阀173减压的富氮液体物流169提供。至LP塔150的回流由物流170提供，该物流170从HP塔的中间位置抽取，经阀171减压，然后送至LP塔150的顶部。
图6中所示过程与图3中所示的相似，辅助塔196具有再沸器/冷凝器161。主要不同在于过程的空气原料。图6中，空气物流100在压缩机102中压缩，并将压缩物流在净化器104中净化以除去水和二氧化碳。将净化的压缩空气物流105分成三股分离的物流107、108和122。
将净化的压缩空气物流108在主换热器112中冷却并将冷却的物流110在膨胀器118中膨胀，为过程提供部分制冷量。将所得膨胀空气流送至HP塔124的底部。
物流122在压缩机123中进一步压缩，生成进一步压缩的原料空气物流126，将该物流126在主换热器112中冷却。然后将该经冷却的进一步压缩的空气在适当的压力调节后以物流128送到HP塔124的中间位置。
将物流107分成两个支流。第一支流在主换热器112中冷却，然后在压力调节后，与来自物流126的经冷却的进一步压缩的空气结合，并以物流128供给HP塔124。第二支流325在主换热器中冷却，生成冷却的原料空气物流127，将该物流127送至辅助塔196的底部。
来自冷凝器161流向LP塔150的富氮液体物流169、来自HP塔124流向冷凝器161的经泵送的LIN物流165、来自HP塔124流向LP塔150的LIN物流170、以及来自HP塔124中间位置流向LP塔150的LIN的流体物流130都穿过至少部分主换热器112，从而调节每种物流的温度以与其所供入的塔中位置的温度更好地匹配。为简单起见，未示出流过主换热器112时的物流，而是以分解形式(as split up)示出了换热器112。
图6中的过程与图3中的不同还在于将LIN物流190和泵送的LOX物流185作为产物流移出。
实施例
已经进行了图6中所示过程的计算机模拟，以例示本发明。该模拟中，辅助塔196只有10个理论级，然而如果以不使不纯氮返回ASU的其余部分来直接生产纯氮将需要约50级。模拟的结果示于表1中。
表1
    原料物流 105   107   108   122     325
    FPT％O2％N2％Ar相 kmol/hbar(MPa)摄氏度℃  1000013.4(1.34)3020.9678.110.93蒸气 291713.4(1.34)3020.9678.110.93蒸气 466713.4(1.34)3020.9 678.110.93蒸气   241613.4(1.34)3020.9678.110.93蒸气     251913.4(1.34)3020.9678.110.93蒸气
    产物流  168 176 185   186     190
    FPT％O2％N2％Ar相 kmol/hbar(MPa)摄氏度℃  252612.5(1.25)271ppm99.890.11蒸气 56931.2(0.12)276.5092.001.50蒸气 4234(3.4)-177.799.8 50.000.15液体   168833.4(3.34)2799.850.000.15蒸气     514.9(0.49)-189.31ppm99.890.11液体
    中间物流  127 165 166   167     169
    FPT％O2％N2％Ar相 kmol/hbar(MPa)摄氏度℃  251912.8(1.28)-16120.9678.110.93蒸气 252612.7(1.27)-170.31ppm99.890.11液体 252612.7(1.27)-165.41ppm99.890.11蒸气   118912.8(1.28)-16133.9064.901.20液体     13302.7(1.27)-164.39.4090.000.60液体
贯穿说明书通篇，关于实施某种功能的构件的内容中的术语“构件”意在指经调整和/或构造以实施该功能的至少一种设备。
可以理解本发明不限于以上参照优选实施方案描述的细节，而是可以进行多种改变或变形而不偏离如以下权利要求所限定的本发明精神和范围。

Claims (26)

1.一种生产加压气态氮(“GAN”)的方法，该方法包含：
在低温空气分离单元(“ASU”)中生产液氮(“LIN”)；
增加至少部分所述LIN的压力以生产加压的LIN；
在辅助低温蒸馏塔中分离氧气浓度至少与空气相同的流体，以生成富氮的塔顶蒸气和浓集氧的塔底液体；
在至少部分所述富氮塔顶蒸气与至少部分所述加压的LIN之间进行传热和任选地传质，以生成富氮的液体和加压GAN；以及
在适当的压力调节后，将至少部分所述富氮的液体作为回流供给ASU。
2.如权利要求1中所述的方法，其中在适当的压力调节后，将至少部分所述浓集氧的液体供给ASU。
3.如权利要求1中所述的方法，其中所述流体是空气。
4.如权利要求1中所述的方法，其中所述流体是来自ASU的富氧流体。
5.如权利要求1中所述的方法，其中将部分所述富氮液体用于回流入所述辅助塔。
6.如权利要求1中所述的方法，其中将所述的部分LIN泵送以增加其压力。
7.如权利要求1中所述的方法，其中热量在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间间接交换，由此将所述富氮塔顶蒸气冷凝生成富氮液体，将所述加压LIN蒸发生成加压GAN。
8.如权利要求7中所述的方法，其中所述热量用再沸器/冷凝器间接交换。
9.如权利要求1中所述的方法，其中在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间直接传热和传质，生成富氮液体和加压GAN。
10.如权利要求9中所述的方法，其中辅助塔具有至少一个主蒸馏区以及位于该主蒸馏区上方的气/液接触促进构件，所述方法包括在所述接触促进构件中使富氮塔顶蒸气与加压LIN直接接触，生成所述富氮液体和加压GAN。
11.如权利要求10中所述的方法，其中所述接触促进构件是另一蒸馏区。
12.如权利要求1中所述的方法，其中所述流体是气态的。
13.如权利要求1中所述的方法，其中所述流体是液体。
14.如权利要求13中所述的方法，其中用位于所述辅助塔贮槽内的再沸器/冷凝器通过与过程物流的间接换热而将至少部分所述液体蒸发。
15.如权利要求1中所述的方法，其中ASU包含较高压(“HP”)蒸馏塔和较低压(“LP”)蒸馏塔，所述HP塔与所述LP塔通过ASU再沸器/冷凝器热连接，所述方法进一步包含：
在所述HP塔中将空气分离成HP富氮塔顶蒸气和富氧塔底液体；
在所述LP塔中将至少部分所述富氧塔底液体分离成LP富氮塔顶蒸气和液氧(“LOX”)；
在所述ASU再沸器/冷凝器中通过与LOX间接换热将至少部分所述HP富氮塔顶蒸气冷却并至少部分冷凝，生成所述LIN；以及
以部分所述LIN回流所述HP塔。
16.如权利要求15中所述的方法，进一步包含在适当的压力调节后，将部分所述富氧塔底液体用作至少部分所述流体。
17.如权利要求15中所述的方法，其中所述辅助塔的操作压力高于所述LP塔的操作压力。
18.如权利要求15中所述的方法，其中所述辅助塔的操作压力高于所述HP塔的操作压力。
19.如权利要求1所述的方法，其中辅助塔的操作压力为0.1MPa(1.0巴)-3.0MPa(30巴)。
20.如权利要求1中所述的方法，其中加压GAN在0.15MPa(1.5巴)-2.5MPa(25巴)的压力下生产。
21.如权利要求1中所述的方法，其中所述加压GAN的纯度为99.9mol％氮-99.9999mol％氮。
22.生产加压GAN的装置，该装置包含：
包含至少一个蒸馏塔的低温ASU，用于生产LIN；
加压构件，用于将LIN加压；
管件，用于将来自生产所述LIN的ASU塔顶的LIN供给加压构件；
包含主蒸馏区的辅助低温蒸馏塔，用于将氧含量至少与空气相同的流体分离成富氮塔顶蒸气和浓集氧的塔底液体；
能使传递进行的构件，用于能够在至少部分所述富氮塔顶蒸气与至少部分所述加压LIN之间传热和任选地传质，以生产富氮液体和加压GAN；
管件，用于将来自加压构件的加压LIN供给能使传递进行的构件；
减压构件，用于降低富氮液体的压力以生产减压的富氮液体；
管件，用于将来自辅助塔的富氮液体供给减压构件；以及
管件，用于将来自所述减压构件的减压富氮液体作为回流供给ASU。
23.如权利要求22中所述的装置，其中能使传递进行的构件是冷凝构件，用于通过与加压LIN的间接换热而使至少部分富氮塔顶蒸气冷凝，生成富氮液体和加压GAN。
24.如权利要求22中所述的装置，其中所述能使传递进行的构件是气/液接触促进构件，用于促进富氮塔顶蒸气与加压LIN之间的直接接触，所述接触促进构件位于辅助蒸馏塔内主蒸馏区上方。
25.如权利要求24中所述的装置，其中接触促进构件是辅助塔内的另一蒸馏区。
26.如权利要求22中所述的装置，进一步包含：
减压构件，用于降低浓集氧液体的压力以生产减压浓集氧液体；
管件，用于将来自辅助塔的浓集氧液体供给该减压构件；和
管件，用于将来自该减压构件的减压浓集氧液体供给ASU。
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