CN108207113A - 获得压缩氮产品的方法及设备 - Google Patents

获得压缩氮产品的方法及设备 Download PDF

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Publication number
CN108207113A
CN108207113A CN201680010982.XA CN201680010982A CN108207113A CN 108207113 A CN108207113 A CN 108207113A CN 201680010982 A CN201680010982 A CN 201680010982A CN 108207113 A CN108207113 A CN 108207113A
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China
Prior art keywords
tower
lower pressure
pressure
residual gas
pressure column
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CN201680010982.XA
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English (en)
Inventor
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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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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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    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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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
    • F25J3/04006—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
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
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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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    • F25J3/04133—Electrical motor as the prime mechanical driver
    • 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
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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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    • 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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    • F25J3/04248—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
    • 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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    • F25J3/04321—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 oxygen
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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Abstract

用于在蒸馏塔***中通过低温分离空气获得压缩氮产品的方法和设备，所述蒸馏塔***具有高压塔(10)及低压塔(11)以及主冷凝器(12)及低压塔塔顶冷凝器(13)，这两者被构造成冷凝蒸发器。将低压塔(11)的塔底液体(28，29)导入低压塔塔顶冷凝器(13)的蒸发室中。使在此形成的气体作为残余气体(30，31)在第一残余气体涡轮机(33)中做功膨胀。将在此产生的机械能用于驱动冷压缩机(36)。由高压塔(10)的塔顶以气态排出第一压缩氮产品流(19)并在主热交换器(8)中加热。由低压塔(11)的塔顶以气态排出另一股氮流(37)，在冷压缩机(36)中压缩到至少等于第一压缩氮产品流(19)在由高压塔(10)排出时的压力的压力，随后作为第二压缩氮产品流(38)在主热交换器(8)中加热。冷压缩机(36)所克服的压力差至少等于在高压塔(10)的塔顶与低压塔(11)的塔顶之间的压力差的三分之二。

Description

获得压缩氮产品的方法及设备
技术领域
本发明涉及根据权利要求1的前序部分的方法。
背景技术
在Hausen/Linde的专著“低温技术(Tieftemperaturtechnik)”(1985年第2版)及Latimer在化学工程进展(Chemical Engineering Progress)中的论文(第63卷，第2期，1967年，第35页)中描述了低温分离空气的一般性基础知识以及双塔设备的详细结构。双塔的高压塔与低压塔之间的热交换关系通常是通过主冷凝器实现的，在其中高压塔的塔顶气体与低压塔的蒸发的塔底液体方向相反地进行液化。
主冷凝器及低压塔塔顶冷凝器在本发明中被构造成冷凝蒸发器。“冷凝蒸发器”是指其中冷凝的第一流体流与蒸发的第二流体流发生间接热交换的热交换器。每个冷凝蒸发器均具有分别由液化通道和蒸发通道组成的液化室和蒸发室。第一流体流在液化室内冷凝(液化)，第二流体流在蒸发室内蒸发。蒸发室和液化室由彼此存在热交换关系的通道的组组成。
这两个冷凝器在此可以各自通过单独的热交换器区块形成，或者也可以通过多个设置在共同的压力容器中的热交换器区块形成。两者可以被构造成单区块或多区块的浴式蒸发器、强制流蒸发器或降膜蒸发器。此外，主冷凝器可以被构造成级联蒸发器，例如在EP1 287 302 B1(＝US 6,748,763 B2)中所述。
“主热交换器”用于在与来自蒸馏塔***的回流的间接热交换中冷却进料空气。其可以由单个或多个并联和/或串联连接的热交换器区段形成，例如由一个或多个板式热交换器区块形成。
US 4,453,957公开了前述类型的方法。在此仅将在残余气体涡轮机中获得的机械能用于制冷。
发明内容
本发明的目的在于提供至少在高压塔压力下允许由低压塔获得氮流并且在此具有特别低的能耗的方法及相应的设备。
该目的通过权利要求1的特征实现。
在此将在第一残余气体涡轮机(33)中产生的机械能至少部分地用于驱动冷压缩机，该冷压缩机在此直接用于压缩氮产品，即例如被施加至大约为高压塔压力或更高压力的低压塔氮产品。
在本发明的范畴内，出人意料地发现，根据本发明的方法以该方法将低压塔氮施加至高压塔氮的压力水平，并且在此在能量上是有利的。作为副作用，得到比较简单的方法，由此还实现比较低的设备复杂性，尤其是对于主热交换器而言。
在根据本发明的方法中，采用以下压力范围：
高压塔(塔顶)：例如12至17巴，优选13至16巴
低压塔(塔顶)：例如6至10巴，优选7至9巴
在本发明中，第一压缩氮产品流及第二压缩氮产品流基本上可以分离地在主热交换器中加热。但是第一压缩氮产品流和第二压缩氮产品流优选在主热交换器上游混合。
在需要时可以由低压塔的氮产品的另一部分形成额外的第三压缩氮流，这是通过将其直接导入主热交换器中并在低压塔压力(减去压力损失)下作为产品排出而实现的。
在第一残余气体涡轮机与冷压缩机之间的能量传输的第一改变方案中，第一残余气体涡轮机与冷压缩机机械连接。这可以通过共同的轴或传动装置实现。
为了产生工艺冷量可以将残余气体涡轮机与发电机或油压制动器机械连接。
在第一残余气体涡轮机与冷压缩机之间的能量传输的第二改变方案中，第一残余气体涡轮机与发电机机械连接，并由电动机驱动冷压缩机；于是将在发电机中产生的能量以电力方式传输至电动机，并由此驱动冷压缩机。
替代性地，被加热至中间温度的残余气体的第二部分可以在第二残余气体涡轮机中做功膨胀，该第二残余气体涡轮机与连接冷压缩机的第一残余气体涡轮机并联连接。于是该第一残余气体涡轮机可以单独连接冷压缩机，第二残余气体涡轮机则连接发电机或耗能制动器。
在高压塔的压力不足的情况下，可以在主热交换器下游在氮压缩机中进一步压缩第一、第二或这两股压缩氮流。这两股压缩氮流优选共同在该氮压缩机中施加至更高的压力。
在此情况下有利的是，通过在由相结合的n级压缩机的前i级形成的主空气压缩机中压缩进料空气，n≥2，i<n，从而在单独的机器中将空气压缩与氮压缩相结合。在此，氮压缩机由所述相结合的n级压缩机的后n–i级形成。例如使用八级压缩机，其后三级至后四级用作氮压缩机。
此外本发明还涉及根据权利要求14的通过低温分离空气获得压缩氮产品的设备。
根据本发明的设备可以通过独立方法权利要求的一个、多个或所有的特征加以补充。
下面依照在附图中显示的实施例更详细地阐述本发明以及本发明的其他细节。
附图说明
图1所示为本发明的第一实施例，其具有单个残余气体涡轮机；
图2所示为第二实施例，其具有两个残余气体涡轮机；
图3所示为图1的改变方案，其具有相结合的压缩机；
图4所示为图1的另一个改变方案，其中分离地加热两股压缩氮产品流；
图5所示为在第一残余气体涡轮机与冷压缩机之间进行电能传输的实施方案；
图6所示为产品压力略低于高压塔压力的改变方案；
图7所示为与图6相似的实施例，但区别在于具有强制流蒸发器；及
图8所示为与图4相似的***，但区别在于具有彼此相邻地布置的塔。
具体实施方式
在图1中，主空气压缩机2通过过滤器1抽吸大气空气(AIR)，并压缩至约15巴的压力。经压缩的进料空气3在预冷装置4中冷却。其可以包括用于间接冷却的再冷器或直接接触冷却器，或者包括这两者。将经预冷的进料空气5在净化装置6中净化，该净化装置通常由一对可切换的吸附器形成。将经压缩、预冷及净化的进料空气7在主热交换器8中冷却至大约为露点，并经由管线9导入高压塔10中。
高压塔10为蒸馏塔***的一部分，该蒸馏塔***此外还具有低压塔11、主冷凝器12及低压塔塔顶冷凝器13。将高压塔10的塔顶气体14的第一部分15导入主冷凝器12的液化室中，并在此至少部分地冷凝。将在主冷凝器12的液化室中形成的液氮16导入高压塔10中，并将其第一部分在此用作回流。将其第二部分17在UKG 18中冷却并输送(49)至低压塔11的塔顶。
将高压塔10的塔顶气体14的第二部分19作为第一压缩氮产品流19经由管线20输送至主热交换器8，并在此加热至大约为环境温度。如图1所示，热的压缩氮21可以在具有再冷器23的氮压缩机22中进一步升高压力，原则上至任何所期望的排出压力。最终将其作为压缩氮产品(PGAN)排出。对于所期望的产品压力不高于高压塔压力(减去压力损失)的情况，可以省略掉氮压缩机22及再冷器23。
由高压塔10的塔底排出液态粗氧24，在UKG 18中冷却，并在中间位置导入低压塔11。将低压塔11的塔顶气体26导入低压塔塔顶冷凝器13的液化室中。将在此形成的液氮27导入低压塔11中。低压塔11的塔底液体28在UKG 18中冷却，并经由管线29导入低压塔塔顶冷凝器13的蒸发室中，其经由冲洗管线39连续或间歇地进行冲洗。将在此形成的气体作为残余气体30在UKG 18中加热。将在UKG 18下游的残余气体31于冷端送入主热交换器8，并在此加热至中间温度。将处于中间温度的残余气体32送入第一残余气体涡轮机33并在此做功膨胀。将经膨胀的残余气体34再次送入主热交换器8中，并直至热端进行加热。经加热的残余气体35大约在环境温度下离开设备。残余气体涡轮机33通过共同的轴或传动装置与冷压缩机36机械连接。
由低压塔11的塔顶以气态排出氮流37，在冷压缩机36中压缩至大约为高压塔压力，经由调节阀41引导，随后作为第二压缩氮产品流38与第一压缩氮产品流19混合，并与其一起在主热交换器8中加热，最后作为压缩氮产品(PGAN)排出。
为了补偿设备的冷量损失，残余气体涡轮机33并非将其全部的机械能输送至冷压缩机36，而是此外还驱动发电机40，该发电机安装在相同的轴上或者连接相同的传动装置。还可以使用耗能制动器例如油压制动器代替发电机40。
在图2中使用两个并联连接的残余气体涡轮机33，233，其中一个连接至冷压缩机36，另一个连接至发电机240(或耗能制动器)。
在图1和2中，主空气压缩机2及氮压缩机22由两***立的机器形成，而在图3的实施例中使用满足这两个目的的相结合的压缩机302。其在该实施例中具有n＝8级，其中i＝5级形成主空气压缩机2。剩下的n–i＝3级形成氮产品压缩机。由此可以达到约70至100巴的PGAN最终压力。
在图4的实施例中，将两股压缩氮产品流19，38在主热交换器8的分离的通道组中加热。经加热的氮流419及438在420处汇合。由此可以将来自冷压缩机36的第二压缩氮产品流38在比第一压缩氮产品流19更高的温度下送入主热交换器8中。由此可以使该过程在能量上略微更加有利。
与图1不同，在图5中在第一残余气体涡轮机33与冷压缩机36之间的能量传输不是以机械方式，而是以电力方式进行。为此，第一残余气体涡轮机33与发电机40机械连接。将在此获得的电能经由电线网络至少部分地传输至电动机540，该电动机又与冷压缩机36机械连接并对其进行驱动。
与图2相比，全部的残余气体在发电机-涡轮机33/40中膨胀，并由此还产生驱动冷压缩机所需的能量。
图2至5的具体特征也可以任意地相互组合，例如组合成包括两个残余气体涡轮机及相结合的压缩机及在主热交换器中用于这两股压缩氮流的两个通道组的***。在所有的实施例中，(具有筛板的)高压塔与(具有填充物或筛板的)低压塔彼此上下布置。替代性地，它们可以彼此相邻地设置。本发明还适合于离岸的方案，例如用于油田或气田的获得氮的漂浮(floating)设备(原油强化回收，enhanced oil recovery–EOR)。
图6基本上对应于图4，但是在此额外的节流阀619位于管线419中。在此所示的改变方案中，在塔顶处高压塔压力为12.0巴时，产品压力为10.9巴。在此将来自低压塔塔顶的氮流37在冷压缩机36中相应地仅压缩至11.1巴，即不完全地压缩至高压塔压力。将其与来自高压塔在节流阀619中节流的氮流419于420处在10.9巴的所期望的压力下汇合。
在此重要的是，在主热交换器8下游进行节流619。由此出人意料地使节流损失大幅最小化，并且可以降低进料空气的压力。也可以在主热交换器8中完全或部分地实施由12.0巴至10.9巴的节流操作，这是通过选择在此处相应地高的压力损失实现的。由此可以特别紧凑地构造主热交换器8。
图7与图6的区别在于，不是使用浴式蒸发器，而是使用强制流蒸发器，作为主冷凝器12及低压塔塔顶冷凝器13。在此情况下，由高压塔10的塔底排出冲洗流701(Purge)。替代性地，还可以使用降膜蒸发器作为主冷凝器12。
在图8中，高压塔10和低压塔11不是如图1至7所示彼此上下布置，而是彼此相邻地布置。在其他方面，图8与图4或图5没有区别，取决于氮产品是在高压塔压力下还是在略微较低的压力下(节流阀619)排出。

Claims (14)

1.在蒸馏塔***中通过低温分离空气获得压缩氮产品的方法，所述蒸馏塔***具有高压塔(10)及低压塔(11)以及主冷凝器(12)及低压塔塔顶冷凝器(13)，这两者被构造成冷凝蒸发器，其中
-将经压缩、预冷及净化的进料空气(7)在主热交换器(8)中冷却并至少部分地导入所述高压塔(10)中，
-将所述高压塔的塔顶气体(14，15)导入所述主冷凝器(12)的液化室中，并将在所述主冷凝器(12)的液化室中形成的液氮(16)的至少一部分导入所述高压塔(10)中，
-将所述低压塔(11)的塔顶气体(26)导入所述低压塔塔顶冷凝器(13)的液化室中，并将在所述低压塔塔顶冷凝器(13)的液化室中形成的液氮(27)的至少一部分导入所述低压塔(11)中，
-将所述低压塔(11)的塔底液体(28，29)导入所述低压塔塔顶冷凝器(13)的蒸发室中，
-将在所述低压塔塔顶冷凝器(13)的蒸发室中形成的气体作为残余气体(30，31)在所述主热交换器(8)中加热至中间温度，使其至少第一部分(32)在第一残余气体涡轮机(33)中做功膨胀，再次送入所述主热交换器(8)中，并直至所述主热交换器(8)的热端进行加热，
-由所述低压塔(11)的塔顶以气态排出氮流(37)，及
-由所述高压塔(10)的塔顶以气态排出第一压缩氮产品流(19)并在所述主热交换器(8)中加热，
其特征在于，
-将在所述第一残余气体涡轮机(33)中产生的机械能至少部分地用于驱动冷压缩机(36)，
-将由所述低压塔(11)的塔顶以气态排出的氮流(37)在所述冷压缩机(36)中压缩到至少等于所述第一压缩氮产品流(19)在由所述高压塔(10)排出时的压力减去2巴的压力，随后作为第二压缩氮产品流(38)在所述主热交换器(8)中加热，及
-将由所述低压塔(11)的塔顶以气态排出的氮流(37)在所述冷压缩机(36)中压缩到至少等于所述第一压缩氮产品流(19)在由所述高压塔(10)排出时的压力减去2巴的压力，随后作为第二压缩氮产品流(38)在所述主热交换器(8)中加热，
-其中所述冷压缩机(36)所克服的压力差至少等于在所述高压塔(10)的塔顶与所述低压塔(11)的塔顶之间的压力差的三分之二。
2.根据权利要求1的方法，其特征在于，将所述第一压缩氮产品流(19)与所述第二压缩氮产品流(38)在所述主热交换器(8)的上游混合。
3.根据权利要求1或2的方法，其特征在于，所述第一残余气体涡轮机(33)通过共同的轴或传动装置与所述冷压缩机(36)机械连接。
4.根据权利要求3的方法，其特征在于，所述第一残余气体涡轮机(33)还与发电机(40)或油压制动器机械连接。
5.根据权利要求1或2的方法，其特征在于，所述第一残余气体涡轮机(33)与发电机(40)机械连接，所述冷压缩机(36)由电动机(540)驱动，在所述发电机(40)中产生的能量至少部分地以电力方式传输至所述电动机(540)。
6.根据权利要求1至5之一的方法，其特征在于，被加热至中间温度的残余气体(32)的第二部分在与所述第一残余气体涡轮机(33)并联连接的第二残余气体涡轮机(233)中做功膨胀。
7.根据权利要求6的方法，其特征在于，所述第一残余气体涡轮机(33)与所述冷压缩机(36)机械连接，所述第二残余气体涡轮机与发电机(240)或耗能制动器机械连接。
8.根据权利要求1至7之一的方法，其特征在于，所述第一压缩氮流、所述第二压缩氮流或这两者在所述主热交换器(8)的下游在氮压缩机(22)中进一步压缩。
9.根据权利要求8的方法，其特征在于，在由相结合的n级压缩机(302)的前i级形成的主空气压缩机(2)中压缩所述进料空气，其中n≥2，i<n，所述氮压缩机(22)由相结合的n级压缩机(302)的后n–i级形成。
10.根据权利要求1至9之一的方法，其特征在于，将由所述低压塔(11)的塔顶以气态排出的氮流(37)在所述冷压缩机(36)中压缩到至少等于所述第一压缩氮产品流(19)在由所述高压塔(10)排出时的压力的压力。
11.根据权利要求1至10之一的方法，其特征在于，所述第一压缩氮产品流(19)和所述第二压缩氮产品流(38)在分离的通道中加热，并尤其是随后汇合。
12.根据权利要求1至11之一的方法，其特征在于，采用以下措施中的至少一个、多个或全部：
-所述主冷凝器(12)被构造成强制流蒸发器，
-所述主冷凝器(12)被构造成降膜蒸发器，
-所述低压塔塔顶冷凝器(13)被构造成强制流蒸发器。
13.根据权利要求1至12之一的方法，其特征在于，
-所述低压塔(11)被布置与所述高压塔(10)相邻，
-所述主冷凝器(12)被布置在所述高压塔(10)上方，及
-所述低压塔塔顶冷凝器(13)被布置在所述低压塔上方。
14.通过低温分离空气获得压缩氮产品的设备，其包括：
-蒸馏塔***，其具有高压塔(10)及低压塔(11)以及主冷凝器(12)及低压塔塔顶冷凝器(13)，这两者被构造成冷凝蒸发器，
包括：
-主热交换器(8)，其用于冷却经压缩、预冷及净化的进料空气(7)，-其中所述主冷凝器(12)的液化室与所述高压塔(10)的塔顶流通连接(14，15，16)，
-所述低压塔塔顶冷凝器(13)的液化室与所述低压塔(11)的塔顶流通连接(26，27)，所述低压塔塔顶冷凝器(13)的蒸发室与所述低压塔(11)的塔底流通连接(28，29)，
及包括：
-用于将在所述低压塔塔顶冷凝器(13)的蒸发室中形成的气体作为残余气体(30，31)排出的装置，
-用于在所述主热交换器(8)中将所述残余气体(31)加热至中间温度的装置，
-用于使经部分加热的残余气体(32)做功膨胀的第一残余气体涡轮机(33)，
-用于将经膨胀的残余气体(34)导入所述主热交换器(8)中的装置及用于由所述主热交换器(8)的热端排出经加热的残余气体的装置，
-将在所述第一残余气体涡轮机(33)中产生的机械能用于驱动冷压缩机(36)的装置，及
-用于由所述高压塔(10)的塔顶排出气态的第一压缩氮产品流(19)以及用于在所述主热交换器(8)中加热所述第一压缩氮产品流(19)的第一压缩氮产品管线，
其特征在于，
-用于由所述低压塔(11)的塔顶排出气态氮流(37)的装置，
-用于将所述气态氮流(37)导入所述冷压缩机(36)中的装置，及
-用于将经冷压缩的氮流作为第二压缩氮产品流(38)导入所述主热交换器(8)中的装置，
-其中所述冷压缩机(36)被构造成其所克服的压力差至少等于在所述高压塔(10)的塔顶与所述低压塔(11)的塔顶之间的压力差的三分之二。
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