CN102538396A - 用于生产高压氮的方法和设备 - Google Patents

用于生产高压氮的方法和设备 Download PDF

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CN102538396A
CN102538396A CN201110414278XA CN201110414278A CN102538396A CN 102538396 A CN102538396 A CN 102538396A CN 201110414278X A CN201110414278X A CN 201110414278XA CN 201110414278 A CN201110414278 A CN 201110414278A CN 102538396 A CN102538396 A CN 102538396A
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pressure
tower
liquid
high pressure
conduit
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CN102538396B (zh
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富田新治
中村幸平
广濑健二
J·博维萨热
B·哈
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/04406—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 using a dual pressure main column system
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    • 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
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    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
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    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
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Abstract

本发明涉及一种用于生产高压氮的方法和装置。这种系统包括：用于将空气压缩并将空气冷却至基本为露点的第一压缩机、高压塔、中压塔、用于在高压塔底部引入经压缩的空气的至少一部分的导管；用于将富氧液体从高压塔底部移出的导管；用于将富氧液体的压力降至中压的第一阀，其中所述中压是在高压和大气压力之间；用于在中压塔的中间位置引入富氧液体的导管；用于将从中压蒸馏塔底部移出的液体的至少一部分的压力降至低压以冷却中压塔的顶部冷凝器并形成废蒸气流的第二膨胀机；用于压缩从中压塔移出的蒸气流、冷却经压缩的蒸气流、并将之引至高压塔底部的冷压缩机；用于加热废蒸气流的热交换器、用于使经加热的流膨胀以产生动力的第一膨胀机；用于从中压塔顶部抽吸液体的导管、用于将所抽吸的液体泵压至高压并在高压塔顶部将它注入的泵；以及用于从高压塔顶部抽吸成品氮的导管。

Description

用于生产高压氮的方法和设备
技术领域
本发明涉及一种用于生产高压氮的方法和设备。
背景技术
在生产加压氮的设备中，氮通常直接在使用压力下生产，例如在5至10巴之间。将压缩成略高于该压力的净化空气蒸馏，从而在蒸馏塔顶部产生氮，而通过“富氧液体”(在蒸馏塔底部由富含氧气的空气形成的液体)的膨胀以及借助这种经膨胀的液体来冷却在蒸馏塔顶部的冷凝器而实现回流。富氧液体由此在约3至6巴之间的压力下蒸发。
若设备的大小适合这样做，则蒸发后的富氧液体通过膨胀机以便将设备维持在冷态(cold state)，但通常这种制冷生产是过量的，这对应于能量的损失。在相反的假设中，通过添加来自外部源的液氮来维持冷态，而蒸发后的富氧液体仅在阀中膨胀并随后穿过热力交换器以起到冷却初始空气的作用。因此，蒸发后的富氧液体的一部分能量在这种情况下还是会损失。
尽管在美国专利4,717,410中所披露的发明(在下文中称为“Grenier循环”)对生产高压氮十分有效，但近年来为了满足客户对高压氮产品的需求，即使采用了Grenier循环，也经常需要通过添加氮压缩机来给成品氮增压。一种可供选择的方案是：可通过增加顶部冷凝器的压力来供应高压氮。但是这种方法使回收率以及比功率降低。
在Grenier专利的图2中，气体从蒸馏塔的下部部分抽吸并送至膨胀机。由于该气体成分类似于空气成分，这意味着这种方法降低了氮回收率。
本发明的一个目的是提供一种工艺流程和装置，以允许以高回收率生产高压氮而无需额外的氮压缩机。
发明内容
本文提供了一种生产高压氮的方法和装置。这种系统包括：用于将空气压缩并将空气冷却至基本为露点的第一压缩机、高压塔、中压塔、用于将经压缩的空气的至少一部分在高压塔底部引入的导管；用于将富氧液体从高压塔底部移出的导管；用于将富氧液体的压力降至中压的第一阀，其中所述中压是在高压和大气压力之间；用于将富氧液体在中压塔的中间位置引入的导管；用于将从中压蒸馏塔底部移出的液体的至少一部分的压力降至低压以冷却中压塔的顶部冷凝器并形成废蒸气流的第二阀；用于压缩从中压塔移出的蒸气流、冷却经压缩的蒸气流、并将之引至高压塔底部的冷压缩机；用于加热废蒸气流的热交换器、用于使经加热的蒸气流膨胀以产生动力的第一膨胀机；用于从中压塔顶部抽吸液体的导管、用于将所抽吸的液体泵压至高压并在高压塔顶部将它注入的泵；以及用于从高压塔顶部抽吸成品氮的导管。
附图说明
图1示出根据本发明的一个实施例的单膨胀机实施例。
图2示出根据本发明的一个实施例的双膨胀机实施例。
具体实施方式
以下说明了本发明的示例性实施例。本发明可有多种修改和变更形式，其具体实施例已在附图中作为范例示出并在本文中详细描述。但是应理解，本文对具体实施例的描述并不意在将本发明限制在所公开的特定形式上，而是相反地，其意在覆盖所有落在由所附权利要求书限定的本发明的精神和范围之内的修改、等价和替代方案。
当然可理解，在开发任一这样的实际实施例时，必须做出众多针对实施的决定以实现开发者的具体目标，例如顺应系统相关和商业相关的约束，所述目标对各个实施例都各不相同。此外，应理解这种开发工作可能是复杂且费时的，但对受益于本公开的本领域技术人员来说不过是一种常规任务。
本发明提供了一种工艺流程和装置以解决前述的缺点。如前文所述，可通过增加顶部冷凝器压力而供应更高压力的氮。但是，更高系统压力也导致氮的回收减少，因为蒸馏塔在较高压力下效率较低。参考图1，废气由导管101从塔顶部抽吸，通过交换器102加热至合适的温度水平，随后在膨胀机103中膨胀，并再次被引入交换器102，在此之后其作为废弃物120离开系统。在更高的废气压力下，由于废气膨胀机103在更高压比下工作，因此需要更少的废气来实现热平衡。因此，为使系统获得改善的性能，必须在更高压力(与Grenier循环相比)下提高成品氮回收率。这种回收率的增加减少了废气流，从而允许系统实现最优热平衡。因此，通过在更高压力下提供改善的氮回收，本系统适于有效地生产高压氮而无需采用额外的氮产品压缩机。
同样，在本发明中，富氧气体(废气)由导管101从顶部冷凝器抽吸并送至膨胀机103以实现热平衡或工艺流程的制冷平衡。由于富氧气体用于热平衡，因此并未改变成品氮回收率。优选地，通过采用膨胀机103，由膨胀机103输出的功的至少一部分可用于运行冷氮压缩机105。从中压蒸馏塔106抽吸成分接近空气的气体。该气体被送至前述的冷氮压缩机105并被加压至与高压塔107近似相等的压力。加压后的气体随后被引入高压蒸馏塔107的底部以提高成品氮回收率。通过提高成品氮回收率，可实现生产成本的降低。
本发明的一个实施例有关于一种设备，该设备具有膨胀机103、热交换器102和双蒸馏塔106、107。蒸馏塔由在高压下(即在生产压力下，约10巴)运行的下部主塔107和在中压(约5巴)下运行的上部副塔106组成。这些塔中的每一个都分别具有顶部冷凝器108、109。
在图1中，经压缩的且除去水分和二氧化碳的空气111，通过热交换器102被冷却至约为它的露点，并被在塔107的底部引入。与塔107底部处接收的进气相平衡的富氧液体112在膨胀阀113中被减压至中压并被在塔106的中间点引入。在中压塔106中，下行液体富集氧气并在塔106底部处冷却主冷凝器108，以确保塔107中的回流。塔106的底部液体140在膨胀阀114中被减压，然后用于冷却顶部冷凝器109并确保塔106中的回流。
液体140在冷凝器109内在约1.7巴表压的压力下蒸发以形成流101，所述流随后在热交换器102内被加热并随后在膨胀机103内膨胀以提供实现热平衡所需的制冷平衡。膨胀之后，气体随后在交换器线路102中被加热从而构成设备的残余气体120。
冷凝器109的冷凝流的一部分由导管116从塔106抽吸并由泵117送回至高压并在塔107的顶部重新注入。
成分接近空气的一股气流被从塔106抽吸并由导管118送至冷压缩机105并被加压至略高于高压塔107的压力。在本文中所使用的术语“冷压缩”指的是这种方法：机械提升气流的压力，所述气流温度比被送至深冷分离系统的环境水平低且以亚环境温度返回到该系统。从塔106抽吸并送至冷压缩机105的气流可在一中间点处在与富氧液体112引入高度相同的高度被抽吸。冷压缩的机械能必须通过制冷来平衡。该气体随后由热交换器102冷却，并被引至蒸馏塔107的底部以改善成品氮的回收。
气态氮流119被从塔107的顶部抽吸，在热交换器102中被加热并作为氮产品被回收。
在本发明的一个实施例中，该装置包括用于将进给空气冷却至基本为其露点的热交换器102、高压蒸馏塔107、中压蒸馏塔106。本发明还包括用于在所述高压蒸馏塔107的底部引入所述经冷却压缩的空气的至少一部分的导管130、用于从所述高压蒸馏塔底部移出富氧液体的导管112、用于将所述富氧液体的压力降至中压的第一阀113，其中所述中压是在所述高压和大气压力之间。该装置还包括：用于在所述中压蒸馏塔106的中间位置引入所述富氧液体的导管132；用于将从所述中压蒸馏塔106底部移出的液体的至少一部分的压力降至低压以冷却所述中压蒸馏塔的顶部冷凝器并形成废蒸气流101的第二阀114。THC(总碳氢化合物)清洗流141同样被从所述中压蒸馏塔的顶部冷凝器移出。本发明包括用于压缩从中压蒸馏塔106移出的蒸气流118的冷压缩机105、用于冷却所述经压缩的蒸气流的热交换器102以及用于将其引至所述高压蒸馏塔底部的导管131。该装置还包括用于加热所述废蒸气流的热交换器102、用于使所述经加热的流膨胀以产生动力的第一膨胀机103；用于从所述中压蒸馏塔106的顶部抽吸液体的导管116、用于将所述被抽吸的液体泵压至所述高压并将其在高压蒸馏塔107的顶部注入的泵117；以及用于从高压蒸馏塔顶部抽吸成品氮的导管119。
以下为上述发明的一个实施例的一个非限制性范例：
具有标称0.82兆帕表压的进气压力的第一实施例：
  流：   111   130   112   119   115   118   134   131
  流率(标立方米/小时)   1000   1000   621   607   607   58   58   58
  压力(兆帕表压)   0.85   0.84   0.84   0.83   0.82   0.432   0.84   0.83
  温度(摄氏度)   55   -166   -166   -171   53   -175   -153   -166
  氮(％)   78.1   78.1   63.1   100.0   100   82.3   82.3   82.3
  氩(％)   0.9   0.9   1.6   0.0   0.0   1.1   1.1   1.0
  氧(％)   21.0   21.0   35.3   0.0   0.0   16.6   16.6   16.6
  流：   116   136   114   101   122   121   120   141
  流率(标立方米/小时)   169   169   393   391   391   391   391   2
  压力(兆帕表压)   0.42   0.83   0.43   0.10   0.10   0.03   0.01   0.10
  温度(摄氏度)   -179   -178   -172   -180   -145   -158   53   -180
  氮(％)   100.0   100.0   44.3   44.6   44.6   44.6   44.6   19.0
  氩(％)   0.0   0.0   2.4   2.4   2.4   2.4   2.4   2.4
  氧(％)   0.0   0.0   53.3   53.2   53.2   53.2   53.2   78.6
具有标称1.00兆帕表压的进气压力的第一实施例：
  流：   111   130   112   119   115   118   134   131
  流率(标立方米/小时)   1000   1000   735   614   614   197   197   197
  压力(兆帕表压)   1.04   1.03   1.03   1.02   1.01   0.54   1.03   1.02
  温度(摄氏度)   55   -163   -163   -168   53   -172   -151   -163
  氮(％)   78.1   78.1   64.6   100.0   100   82.7   82.7   82.7
  氩(％)   0.9   0.9   1.5   0.0   0.0   1.0   1.0   1.0
  氧(％)   21.0   21.0   32.9   0.0   0.0   16.3   16.3   16.3
  流：   116   136   114   101   122   121   120   141
  流率(标立方米/小时)   152   152   386   384   384   384   384   2
  压力(兆帕表压)   0.54   1.02   0.54   0.15   0.15   0.03   0.01   0.15
  温度(摄氏度)   -176   -176   -169   -178   -140   -159   53   -178
  氮(％)   100.0   100.0   43.3   43.4   43.4   43.4   43.4   19.2
  氩(％)   0.0   0.0   2.4   2.4   2.4   2.4   2.4   2.5
  氧(％)   0.0   0.0   54.3   54.2   54.2   54.2   54.2   78.3
本发明的一个实施例有关于一种设备，该设备具有第一膨胀机204、第二膨胀机203、热力交换器202和双蒸馏塔206、207。蒸馏塔由运行在高压(即在生产压力下，约10巴)的下部主塔207和运行在中压(约5巴)的上部副塔206组成。这些塔中的每一个都分别具有顶部冷凝器208、209。
在图2中，经压缩且除去水分和二氧化碳的空气211，通过热交换器202被冷却至约为它的露点，并被在塔207的底部引入。与塔207底部处接收的进气相平衡的富氧液体212在膨胀阀213中被减压至中压并被在塔206的中间点引入，在中压塔206中，下行液体富集氧气并在塔206底部处冷却主冷凝器208，以确保塔207内的回流。塔206的底部液体240在膨胀阀214内被减压，然后起到冷却顶部冷凝器209的作用并确保塔206中的回流。
成分接近空气的一股气流被从塔206抽吸并由导管218送至冷压缩机205并被加压至略高于高压塔207的压力。随后气体由热交换器202冷却，并被引至蒸馏塔207的底部以改善成品氮的回收。通过提高成品氮回收率，可实现生产成本的降低。
废气由导管201从顶部冷凝器209抽吸、在热交换器202内被加热至适当的温度水平，废气的第一部分221在第一膨胀机204中膨胀，由此产生第一膨胀流223。THC清洗流241同样从所述中压蒸馏塔的顶部冷凝器移出。而炽热废气的第二部分222在第二膨胀机203中膨胀，由此产生第二膨胀流224。第一部分221和第二部分222的温度并不相同。在一个实施例中，第二部分222的温度大于第一部分221的温度。
第一膨胀线路223和第二膨胀线路224可重新合并且再次被引入热交换器202，在此之后其作为废弃物220离开该系统。由第二膨胀机203(或第一膨胀机204)输出的功的至少一部分可用于操作冷氮压缩机205。
液体240在冷凝器209中在约1.7巴表压的压力下蒸发以形成流201，所述流随后在热交换器202内被加热并随后在膨胀机203中膨胀以提供实现热平衡所需的制冷平衡。膨胀之后，气体随后在交换器线路202中被加热从而构成设备的残余气体220。
冷凝器209的经冷凝的流的一部分由导管216从塔206抽吸并由泵217送回至高压并在塔207的顶部重新注入。气态氮流219被从塔207的顶部抽吸，在热交换器202内被加热并作为氮产品被回收。
本领域技术人员应认识到，可以有额外的膨胀机配置，且不应局限于图1和图2所示的方案。除了改善热交换器202中的温度水平之外，双膨胀机配置还提供了使第二膨胀机203的入口温度更高的优势，这从它的输出功的角度来讲是有益的。更高的输出功意味着更多流可被回收利用以及更高的产品回收率。应注意同样有用的是，在图1的方案中，由膨胀机103产生并用于抵消工艺流程所需制冷的过量制冷可例如在一体化的油压制动器或发电机制动器(未示出)中消耗。
在本发明的一个实施例中，该装置包括用于将进给空气冷却至基本为其露点的热交换器202、高压蒸馏塔207、中压蒸馏塔206。本发明还包括：用于在所述高压蒸馏塔底部引入所述经压缩的空气的至少一部分的导管230；用于将富氧液体从所述高压蒸馏塔207底部移出的导管212；以及用于将所述富氧液体的压力降至中压的第一阀213，其中所述中压是在所述高压和大气压力之间。本发明还包括：用于在所述中压蒸馏塔206的中间位置引入所述富氧液体的导管232；用于将从所述中压蒸馏塔底部移出的液体的至少一部分的压力降至低压以冷却所述中压蒸馏塔206的顶部冷凝器并形成废蒸气流的第二阀214。本发明还包括用于将从中压蒸馏塔206移出的蒸气流压缩、将所述经压缩的蒸气流冷却、并将其引入至所述高压蒸馏塔207底部的冷压缩机205。本发明还包括用于加热所述废蒸气流的热交换器202、用于使所述经加热蒸气流的一部分膨胀以产生动力的第一膨胀机203；以及用于使所述经加热蒸气流的另一部分膨胀以产生动力的第二膨胀机204。本发明还包括：用于从所述中压蒸馏塔206的顶部抽吸液体的导管216；用于将所抽吸的液体泵压至所述高压并将其在高压蒸馏塔207顶部注入的泵217；以及用于从高压蒸馏塔顶部抽吸成品氮的导管219。
具有标称0.82兆帕表压的进气压力的第二实施例：
Figure BDA0000119426590000081
Figure BDA0000119426590000082
Figure BDA0000119426590000091
具有标称1.00兆帕表压的进气压力的第二实施例：
Figure BDA0000119426590000093

Claims (7)

1.一种用于生产高压氮的方法，所述方法包括：
将进给空气冷却至基本为其露点；
在高压塔的底部引入所述空气的至少一部分；
将富氧液体从所述高压塔的底部移出；
将所述富氧液体的压力降至中压，其中所述中压在所述高压和大气压力之间；
在中压塔的中间位置引入所述富氧液体；
将从所述中压塔的底部移出的液体的至少一部分的压力降至低压以冷却所述中压塔的顶部冷凝器并形成废蒸气流；
在冷压缩机中压缩从中压塔移出的蒸气流，冷却所述经压缩的蒸气流，并将它引入到高压塔的底部中；
加热所述废蒸气流，并使所述经加热的流膨胀以产生动力；
从所述中压塔的顶部抽吸液体；
将所抽吸的液体泵压至所述高压并在高压塔的顶部将它注入；以及
从高压塔的顶部抽吸成品氮。
2.根据权利要求1所述的方法，其特征在于，所述动力的至少一部分由所述冷压缩机利用。
3.一种用于生产高压氮的装置，所述装置包括：
用于将进给空气冷却至基本为其露点的热交换器；
高压蒸馏塔；
中压蒸馏塔；
用于在所述高压蒸馏塔的底部引入所述经冷却压缩的空气的至少一部分的导管；
用于将富氧液体从所述高压蒸馏塔的底部移出的导管；
第一阀，所述第一阀用于将所述富氧液体的压力降至中压，其中所述中压是在所述高压和大气压力之间；以及
用于在所述中压蒸馏塔的中间位置引入所述富氧液体的导管；
第二阀，所述第二阀用于将从所述中压蒸馏塔底部移出的液体的至少一部分的压力降至低压以冷却所述中压蒸馏塔的顶部冷凝器并形成废蒸气流；
用于压缩从中压蒸馏塔移出的蒸气流的冷压缩机，用于冷却所述经压缩的蒸气流的热交换器，以及用于将它引入到所述高压蒸馏塔的底部中的导管；
用于加热所述废蒸气流的热交换器；
第一膨胀机，所述第一膨胀机用于使所述经加热的流膨胀以产生动力；
用于从所述中压蒸馏塔顶部抽吸液体的导管；
用于将所抽吸的液体泵压至所述高压并在高压蒸馏塔顶部将其注入的泵；以及
用于从高压蒸馏塔的顶部抽吸成品氮的导管。
4.一种用于生产高压氮的方法，所述方法包括：
将进给空气冷却至基本为其露点；
在高压塔的底部引入所述空气的至少一部分；
将富氧液体从所述高压塔的底部移出；
将所述富氧液体的压力降至中压，其中所述中压在所述高压和大气压力之间；
在中压塔的中间位置引入所述富氧液体；
将从所述中压塔的底部移出的液体的至少一部分的压力降至低压以冷却所述中压塔的顶部冷凝器并形成废蒸气流；
在冷压缩机中压缩从中压塔移出的蒸气流，冷却所述经压缩的蒸气流，并将它引入到高压塔的底部中；
将所述废蒸气流的一部分加热至第一温度，并在第一膨胀机中使所述经加热的流膨胀以产生动力；
将所述废流的另一部分进一步加热至第二温度，并在第二膨胀机中使所述经进一步加热的流膨胀以产生动力；
从所述中压塔的顶部抽吸液体；
将所抽吸的液体泵压至所述高压并在高压塔的顶部将它注入；以及
从高压塔的顶部抽吸成品氮。
5.根据权利要求4所述的方法，其特征在于，所述动力的至少一部分由所述冷压缩机利用。
6.根据权利要求1所述的方法，其特征在于，所述富氧液体在与被从所述中压塔移出的并在所述冷压缩机中压缩的所述蒸气流相同的高度被引入。
7.一种用于生产高压氮的装置，所述装置包括：
用于将进给空气冷却至基本为其露点的热交换器；
高压蒸馏塔；
中压蒸馏塔；
用于在所述高压蒸馏塔的底部引入所述经压缩的空气的至少一部分的导管；
用于将富氧液体从所述高压蒸馏塔的底部移出的导管；
第一阀，所述第一阀用于将所述富氧液体的压力降至中压，其中所述中压是在所述高压和大气压力之间；以及
用于在所述中压蒸馏塔的中间位置引入所述富氧液体的导管；
第二阀，所述第二阀用于将从所述中压蒸馏塔底部移出的液体的至少一部分的压力降至低压以冷却所述中压蒸馏塔的顶部冷凝器并形成废蒸气流；
冷压缩机，所述冷压缩机用于压缩从中压蒸馏塔移出的蒸气流，冷却所述经压缩的蒸气流，并将它引入到所述高压蒸馏塔的底部中；
用于加热所述废蒸气流的热交换器；
第一膨胀机，所述第一膨胀机用于使所述经加热的流的一部分膨胀以产生动力；
第二膨胀机，所述第二膨胀机用于使所述经加热的流的另一部分膨胀以产生动力；
用于从所述中压蒸馏塔顶部抽吸液体的导管；
用于将所抽吸的液体泵压至所述高压并在高压蒸馏塔顶部将其注入的泵；以及
用于从高压蒸馏塔的顶部抽吸成品氮的导管。
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