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CN1105443A - 氧和氮作为气态和/或液态产品共同生产的分离方法 - Google Patents

氧和氮作为气态和/或液态产品共同生产的分离方法 Download PDF

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Publication number
CN1105443A
CN1105443A CN94115300A CN94115300A CN1105443A CN 1105443 A CN1105443 A CN 1105443A CN 94115300 A CN94115300 A CN 94115300A CN 94115300 A CN94115300 A CN 94115300A CN 1105443 A CN1105443 A CN 1105443A
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tower
air
logistics
liquid
oxygen
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CN94115300A
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J·G·徐
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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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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    • F25J3/02—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
    • F25J3/04024—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 purified feed air, so-called boosted air
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    • 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
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    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
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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
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
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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
    • 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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Abstract

本发明为一种低温蒸馏方法的改进方法，该方法 用于将空气分离成其组成成分。该方法采用一套具 有至少两个蒸馏塔的蒸馏塔系统，其中，高压塔的顶 部与低压塔热交换连通。本改进方法的特征在于： (a)通过适宜的手段将一部分压缩干燥且无污染的进 料空气冷凝，如经液态氧的蒸发或其它冷冻源；(b) 将至少一部分液态空气物流作为不纯的回流液加至 蒸馏塔系统的一个蒸馏塔中；和(c)从蒸馏塔中排出 废蒸气物流，排出点在蒸馏塔中的位置位于向蒸馏塔 系统中加入步骤(b)的液态空气物流的位置上方不 超过四个理论级处，从而在废蒸气物流的氮摩尔分数 小于0.95。

Description

本发明涉及一种通过低温蒸馏空气来生产氮和氧的方法。
用于生产氧的空气分离方法中最常采用及众所周知的方法是本世纪上半时发明的林德双塔循环法。这种方法的基本原理是使高压塔的顶部与低压塔底部热连通从而使来自高压塔的蒸气氮冷凝以及使低压塔底部的液态氧再沸腾。然后将从高压塔得到的一部分液氮作为回流液加至低压塔的顶部。这种空气分离工厂能回收空气进料中90%以上的氧，从而由低压塔得到的蒸气所含氮超过97%。当要求大量的氮气作为副产物以及氮气须满足一定纯度要求时，需要在低压塔顶部的下面设置许多塔盘以从中排出废物物流以便于控制氮气产品的纯度。而这种废物物流仍可包含超过95%的氮以使氧及氩的回收率保持相当高。这种废物物流的流量通常限制为小于15%，这使得足以使用温度转换吸附减析技术来再生分子筛吸附床。
当需要大量生产液体时，常规方法是采用一种冷冻系统，其中用氮气作为工作流体，这种系统生产液氮，其可作为产品和/或用于空气分离单元的附加回流液，所说的单元依然为具有上述特征的林德双塔系统，如US 3，605，422所述，当液体/进料比相当小时，也可使用的空气作为工作流体的冷冻系统。这种液化器是使用使一部分高压空气膨胀来压缩另一部分高压空气的冷冻技术。而空气分离单元仍然是具有上述特征的林德双塔循环，如US 4，152，130所述。
由于上述方法均使用传统的林德双塔循环，这种循环可实现空气基本完全的分离而得到氧气和氮气（在某些应用中还有氩气），如果几乎所有的空气分离产品即氧气和氮气（和氩气）均是需要的话：这种方法是适宜的。然而，在大多数情形下，由空气分离厂生产的大部分氮气没有什么用途（除了在废物塔中用于冷却水）。相应地，一些氮气产品在其从低温箱排出后向大气中排放。在另外一些时候，一些气体产品也被要求作为液体产品。在其它一些情形下，可使用更好的循环来减少能源消耗以及空气分离单元的基本投资。
US 5，165，245公开了一种采用高压双塔系统的方法。在该方法中，使用高压氮膨胀的冷冻技术来生产液态产品。这种高压方法的效能体现在压降损失减少，加工设备如管路及热交换器的尺寸减小。但不幸的是，如果不生产液态产品或不需要液态产品，那么这种方法将是不适宜的。
本发明的方法涉及一种低温蒸馏方法的改进方法，该方法用于将压缩的干燥且无污染的空气分离成其组成成分，该方法采用一套具有至少两个在不同压力下操作的蒸馏塔的蒸馏塔系统，其中，高压塔的顶部与低压塔热交换连通，其中，氮产品在高压塔的顶部产生，氧产品在低压塔的底部产生，本改进方法的特征在于：（a）一部分压缩的干燥且无污染的进料空气被压缩而产生液态空气物流;（b）将至少一部分液态空气物流作为不纯的回流液加至蒸馏塔系统的至少一个蒸馏塔中;和（c）从蒸馏塔中排出氮摩尔分数小于0.95的废蒸气物流，排出点在蒸馏塔中的位置位于向该蒸馏塔系统中加入步骤（b）的液态空气物流的位置上方不超过四个理论级处。
在本发明方法的优选实施方式中，步骤（b）的液态空气物流被加至低压塔的顶部，而步骤（c）的废蒸气物流是从该低压塔的顶部排出。同样，另一部分步骤（a）的液态空气可加至高压塔的中间位置，而另一部分废蒸气物流从高压塔的某一位置排出，该位置位于向高压蒸馏塔中加入另一部分液态空气的位置上方不超过四个理论级处。
进而，步骤（a）的部分原料空气经下述热交换过程而被冷凝，与离开加工过程的温热加工物流热交换，或者与低压塔底部的沸腾液态氧进行热交换，或通过上述两种热交换过程。
图1～4为本发明方法的几种实施方式的示意图。
图5和6为本发明方法带有液化器循环过程的两种实施方式的示意图。
图7为US 5，165，245公开的现有技术的方法示意图。
本发明为一种低温蒸馏方法的改进方法，该方法用于将空气分离成其组成成分。该方法采用一套具有至少两个蒸馏塔的蒸馏塔系统，其中，高压塔的顶部与低压塔热交换连通。本改进方法的特征在于：（a）通过适宜的手段将一部分压缩的干燥且无污染的进料空气冷凝，如经液态氧的蒸发或其它冷冻源;（b）将至少一部分液态空气物流作为不纯的回流液加至蒸馏塔系统的一个蒸馏塔中;和（c）从蒸馏塔中排出废蒸气物流，排出点在蒸馏塔中的位置位于向蒸馏塔系统中加入步骤（b）的液态空气物流的位置上方不超过四个理论级处，从而使该废蒸气物流的氮摩尔分数小于0.95。为了更好地理解本发明，以下将讨论本发明的12种具体实施方式。
图1展示了一种适于生产高压氧、高压氮、以及液态氩和一定量（少于进料空气的10%）的液态氧和液氮的实施方式。在该实施方式中，压缩的干燥且无污染的空气物流100首先被成两部分102和120。第一部分102在主换热器910和911中被冷至温度接近其露点，然后经管路110加至高压塔920的底部。第二部分120在压缩机900中这一步压缩至高压，将这部分高压空气124进一步分成两部分亚物流126和123。第一部分亚物流126在主热交换器910和911中冷却并冷凝从而产生液态空气132，将其在较温热的亚低温冷却器912中进一步作亚低温冷却，将其与在低压塔921中冷凝的液态空气144合并，在更冷的低温冷却器913中进一步冷却，减压后经管路136加至低压塔921的顶部。另一部分亚物流123经压缩机901压缩并在主热交换器910的上部冷却并在膨胀器902中膨胀至一适量的压力，在本实施方式中，压缩机901和膨胀器902之间机械连接。膨胀器的排出物142在位于低压塔921底部的沸腾器/冷凝器914中经液态氧气化而进行的热交换被冷凝。所得到的液态空气144与来自较温热的低温冷却器912的液态空气合并在一起。
在高压塔920中，进料空气110被蒸馏合成高压氮塔顶馏出物和富氧的塔底产物液体。一部分氮塔顶馏出物作为气态氮物流30回收，在热交换器912、911和910中加热以回收冷冻作用（recover refrigeration），并作为高压气态氮产物（HPGAN）300回收。其余的高压氮塔顶馏出物在位于低压塔921的底部的再沸器/冷凝器915中被冷凝。冷凝后的液氮的一部分作为回流液返回高压塔的顶部。而另一部分10在较冷的低温冷却器913中被低温冷却，并在分离器930用闪蒸并进行相分离。液体部分作为液氮产品经管路700排出，气相部分16与废氮40合并并在热交换器913、912、911和910中加热以回收冷量并作为废气400排空。富氧底液体80被排出、减压并经管路84加至低压塔921的中间位置。
被加至低压塔921的进料物流被蒸馏而产生废氮气40和液态氧塔底产物。废氮气40包含少于95%的氮气，这它与来自相分离器930的氮蒸气16混合。经管路20排出液态氧并分成两部分22和50。第一部分50在较冷的低温冷却器913中低温冷却并作为液态氧产品经管路500排出。另一部分22在泵903中用泵增压至一适宜的压力，在主热交换器911和910中被加热并气化，作为高压气态氧产品（HPGUX）200排出。
在本实施方式中，也示出了一个用于生产氩的旁塔。该旁塔（side arm column）922从低压塔921底段的上部位置排出蒸气，并将富氧液体从旁塔922返回至上述同一位置。经中间液体向低压塔下面运行而提供旁塔922的生产量。排出液体氩物流60，在较冷的低温冷却器913中低温冷却，随后作为液态氩产品600排出。
需要指出，当需要大量的加压氮时，可将膨胀器排出物142与冷却后的进料空气106合并，直接将它们加至高压塔920的底部。这种选择方式在图2中示出。除了上述变化外。图2所示的实施方式的其它部分与图1所示是相同的。
这种思路可用于生产低纯氧。图3示出了如何使用一个双沸腾器空气分离单元来生产低纯氧和加压氮。在该实施方式中，首先将压缩干燥且无污染的空气100分成两部分102和130。较少的一部分130在压缩机901中再次压缩，在主热交换器910中冷却并在膨胀器902中膨胀。膨胀器排出物138被加至低压塔921的上中部。在本实施方式中，压缩机901和膨胀器902机械连接。主要部分102在主热交换器910中冷却至其温度接近其露点，并将其分成两部分亚物流。第一部分亚物流108被加至高压塔920的底部。第二部分亚物流110在位于低压塔921底部的沸腾器/冷凝器914中经液态氧沸腾而被冷凝。产生的液态空气物流112再被分成两部分114和116。较少的一部分物流114作为不纯回流液被加至高压塔920的中部。大部分的物流116在较冷的低温冷却器913中被低温冷却，闪蒸后作为液体回流液加至低压塔921的顶部。
加至高压塔920的进料空气被分离成高压氮气塔顶馏出物和富氧塔底产物液体。一部分氮气塔顶馏出物在沸腾器/冷凝器916中冷凝并作为回流液加至高压塔920的顶部。其余的氮气塔顶馏出物经管路30排出，并在热交换器912和910中加热以回收冷冻作用，然后作为气态氮产品（GAN）300回收。来自高压塔的富氧塔底产物液体10在较热的低温冷却器912中低温冷却，减压，并经管路14加至低压塔921。
加至低压塔的进料被蒸馏并分离成蒸气物流和氧塔底产物液体。塔921顶部排出的蒸气物流40包含小于95%的氮气，将其热交换器913、912和910中加热以回收冷冻作用，并作为废氮气产品400排出。从塔921底部排出的气态氧在热交换器912和910中加热以回收冷量并作为气态氧产品（GOX）200回收。
图4给出了类似图3的实施方式但包含泵增加LOX过程的实施方式。在该实施方式中，较少一部分130首先在压缩机900中被加缩至高压，然后分离成两部分。第一部分146在主热交换器910中被冷却和冷凝。在较热的亚低温冷却器912中被亚低温冷却，然后与来自沸腾器/冷凝器914的液态空气115合并。合并后的液态空气压更冷的低温冷却器913中进一步冷却，减压后经管路120作为回流液加至低压塔。同样，液态氧20用泵903被泵增加至一适宜的压力。加热以回收冷量，气化后作为气态氧产品200回收。除了上述变化外，图4所示的实施方式的其它部分与图3所示的实施方式相同。
图5的一种用于生产大量液态产品（大于进料空气的10%）的实施方式。在该实施方式中，压缩的干燥且无污染的进料空气90与循环空气800合并。该合并后的空气物流92由压缩机900进一步压缩。然后经压缩机901进一步压缩。将其再次冷却后，该高压空气物流103被分成两部分104和154，再分别通过压伸器压缩机902和903将它们进一步压缩至其压力高于空气的临界压力。然后将压缩机902和903的排出物合并，合并后的物流107再被冷却至接近环境温度的温度。在接近环境温度时，将上述临界压力空气物流分成两部分110和130。第一部分110在热交换器910中被冷却，再分成两部分亚物流114和140。第二部分130在膨胀器904中膨胀并在热交换器910中加热以回收冷冻作用。这种加热且膨胀的第二部分包含再循环物流800。第一部分的第一种亚物流114在热交换器911和912中被进一步冷却至低于空气临界温度的温度。这种低于临界温度的稠密流体空气117再分成两部分118和119。第二种亚物流140在膨胀器905中膨胀并再分成两部分136和138。第一种亚物流的第一部分119被减压后作为不纯回流液加至高压塔920的中间位置。第一种亚物流的第二部分118在低温冷却器913和915中低温冷却，在稠密流体膨胀器907中膨胀，然后经管路126加至低压塔921的顶部。第二种亚物流的第一部分138作为原料加至高压塔920的底部。第二种亚物流的第二部分136在热交换器912和911中加热以回收冷冻作用，然后与膨胀器904的排出物133合并。
加至高压塔920的进料在高压塔内分离，从中排出三种物流。排出的液态氮物流2在较冷的低温冷却器915中低温冷却后，减压并在相分离器930中进行相分离。蒸气相6从相分离器930中排出并与来自低压塔921的废氮气30合并。液相500从相分离器930中作为液氮（LIN）产品排出。富氮蒸气物流20从高压塔920的顶部或塔顶下面几块塔盘处排出。该富氮物流20在热交换器913和912中加热，在膨胀器906中膨胀，在热交换器911和910中进一步加热至环境温度，并作为气态氮产品（GAN）200回收，来自高压塔的富氧塔底产物液体10在较热的亚低温冷却器913中亚低温冷却，减压，在低温冷却器914中用于LOX低温冷却，然后经管路16加至低压塔921中。
加至低压塔921的进料在塔中蒸馏，从低压塔921排出三种物流。废氮气物流30包含少于95%的氮气，它以塔中排出并与来自相分离器930的蒸气相合并，形成的蒸气相310加热回收冷量，以接近环境温度的温度作为废气300从整个工艺过程中排出。从塔中排出的液态氧40在低温冷却器914中低温冷却，并作为液态氧（LOX）产物400回收。最后，富氩蒸气相从低压塔高于塔底的一段处排出，将其加至旁塔的塔底，该旁塔将其蒸馏成液态富氧物流60和富氧塔底产物液体，将其返回低压塔，返回位置为从该处将蒸气加至旁塔的位置。旁塔冷凝器是与低压塔一体的，从而使来自旁塔塔顶的氩蒸气经下述位置下几个塔盘处液体的部分气化而冷凝，所说位置是来自高压塔的富氧塔底产物液体16加至低压塔的位置。富氩液态物流60在排出系统前经低温冷却器冷却。
图5的实施方式表明了液体产率超过20%进料空气的情形。当液体制备量较少时，某些再循环物流（136和800）可反向，加至高压塔的液态空气进料119可省去，如图6所示的实施方式所示。
本发明通过下述手段使蒸气相的氮摩尔分数小于95%，从而使废气物流中的氧量显著降低，所说手段包括：生产液态空气物流并将其作为不纯回流液物流加至某一蒸馏塔中，从液态空气加至塔内的塔盘处或高于该塔盘四个塔盘以下的塔盘处排出大量的蒸气。本发明的方法不同于在氧分离工厂常规的设计和操作方法，其中氧回收率最大。本发明的这些方法比传统方法有以下的优点（传统方法如图7所示）：
（1）由于每分离1摩尔的氧的最小功耗在低回收率时要小于高回收率时。因而，本发明具有能量效益。例如，当85.9%的进料空气中的氧被回收作为氧产品时（按照本发明的方法），与传统方法所有的氧回收相比，分离每1摩尔氧的最小功耗要少8.35%。
（2）当大量（15～30%的进料空气）的氮需作为加压产品（输出压力（deliuery pressure）略低于高压塔压力和略高）时，或者当大量的进料空气作为液态产品排出（＞10%）时，本发明可节约压缩机械。
实施例
为了说明本发明效果和与常用的方法作一比较，做了下述计算机模拟的实施例：这些模拟的结果说明了上述观点下述这些实施例是基于下列生产要求：
产品 纯度:体积% 压力 流速比*
氧气  >99.5  178  1.0
氮气  >99.99  81  1.46
粗液态氩  >99.5  更可能多
液氮  >99.99  0.023
液氧  >99.5  0.032
*流量比定义为:摩尔流速/氧气摩尔流速
用于模拟的生产流程是图1和图7。图1是本发明方法的一种实施方式。图7是具有美国专利5，165，245中所公开的基本上全部回收的方法，模拟的结果列于表1和表4中。
Figure 941153002_IMG2
从表1可以看出方法中可以省去氮气压缩机，用增压器和二个装有发动机并具有压伸器的膨胀器替代氧气压缩机。另外还减少塔盘数并由此可以缩短冷却箱。表2的数据表明图1流程中所用的分子筛床几乎大了17%。氩气回收率较小，而生成的氩气的绝对量却没有明显地减少。本发明氩气的回收率相当于全部氧气回收的常用方法的氩气回收率的80%。在能耗上，图1的方法降低了2.1%。如果仅使用气体分离所需的能量，则该方法将节省能耗4%，这是一个很了不起的数值。
另外需要指出的是，在用于图1所述方法的模拟条件中，高压塔中的回流比较高，这意味着对于一定的氮气纯度所需的塔盘数减少。因此可以分离出更多的氮气并增加高压塔中的塔盘数。但是，氩气的回收率将进一步减少，和氧气的纯度（或回收率）也将会降低。
另外还应注意到，图7所述的方法当其在高压下操作时是已知的同时生产氧气和氮气的最佳现有技术，因为，高压生产方法从分离能力上说其效率要比常用的低压生产方法高出约8%。本发明的累计分离能力要比常用的低压方法高出12%。重要的是，如果不需要所有的氮气为加压产品，则为了有效地运用能量，高压生产方法需要生产一定量的液态产品。但是，本发明的方法也是在不产生液体的条件下进行的。在这种情况下，可以和本发明的方法进行比较的生产方法仅仅是常用的低压生产方法，本发明的方法的分离能力（从分离所需的能量上来看）要比常用的低压生产方法高出12%。
模拟用的一些物流参数列于表3和表4，模拟的基础是以100lboml/小时进料空气。
Figure 941153002_IMG3
本文中运用了几个具体的本发明的实施方式来说明本发明。这些实施方式不能被看成为是对本发明保护范围的限定，本发明的保护范围应由下述权利要求来确定。

Claims (7)

1、一种低温蒸馏方法，该方法用于将压缩的干燥且无污染的空气分离成其组成成分，该方法采用一套具有至少两个在不同压力下操作的蒸馏塔的蒸馏塔系统，其中，高压塔的顶部与低压塔热交换连通，其中氮产品在高压塔的顶部产生，氧产品在低压塔的底部产生，其特征在于：(a)一部分压缩的干燥且无污染的进料空气被压缩而产生液态空气物流；(b)将至少一部分液态空气物流作为不纯的回流液加至蒸馏塔系统的至少一个蒸馏塔中；和(c)从蒸馏塔中排出摩尔分数小于0.95的废蒸气物流，排出点在蒸馏塔中的位置位于向蒸馏塔系统中加入步骤(b)的液态空气物流的位置上方不超过四个理论级处。
2、按权利要求1的方法，其中，步骤（b）的液态空气物流被加至低压塔的顶部，步骤（c）的废蒸气物流从该低压塔的顶部排出。
3、按权利要求2的方法，其中，另一部分步骤（a）的液态空气加至高压塔的中间位置。
4、按权利要求3的方法，其中，另一部分废蒸气物流从高压塔的某一位置排出，该位置位于向高压蒸馏塔中加入另一部分液态空气的位置上方不超过四个理论级处。
5、按权利要求1的方法，其中步骤（a）的进料空气与离开加工过程的温热加工物流热交换而被冷凝。
6、按权利要求1的方法，其中步骤（a）的进料空气与低压塔底部的沸腾液态氧热交换而被冷凝。
7、按权利要求1的方法，其中步骤（a）的进料空气与离开加工过程的温热加工物流热交换和与低压塔底部的沸腾液态氧热交换而被冷凝。
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