CN1100514A - 用于在压力下生产氧的方法及装置 - Google Patents

用于在压力下生产氧的方法及装置 Download PDF

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CN1100514A
CN1100514A CN94101375A CN94101375A CN1100514A CN 1100514 A CN1100514 A CN 1100514A CN 94101375 A CN94101375 A CN 94101375A CN 94101375 A CN94101375 A CN 94101375A CN 1100514 A CN1100514 A CN 1100514A
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air
mentioned
pressure
high pressure
turbine
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CN1101924C (zh
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M·格伦尼尔
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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
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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
    • F25J3/04078—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
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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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    • F25J3/04012—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
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    • Y10S62/939—Partial feed stream expansion, air
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Abstract

被蒸馏的全部空气加压到第一高压，然后分成两 部分。第一部分为待蒸馏的全部空气流的至少 70％，升压到第二高压，在换热器中冷却降到一中间 温度，其中的一部分在平均压力下透平化，而其余部 分被液化。第二部分在换热管中冷却并被液化成压 力在上述第一高压和上述第二高压之间的一个或几 个压力的一个或多个物流。

Description

本发明是关于一种通过空气在双塔设备中进行蒸馏来制备高压气态氧的方法，该双塔设备包括一在平均压力下操作的平均压力塔和一在低压操作下的低压塔，该方法包括泵送低压塔的底部排出的液态氧的步骤，和在装置的换热管中通过与空气换热来使压缩的液态氧气化的步骤。
下文中，术语“冷凝”应当广义理解，即也包括在超临界压力下的假冷凝。
FR-A-2，674，011描述这种类型的方法，在该方法中，所有的空气都是加压到一个高压，此后在平均压力下被冷却并部分地被透平化（turbined）。
本发明旨在改进这种已知的方法，以便提高它的热力学性能，而不增加相应的投资。
为此，本发明的一个目的是提供上述类型的一种方法，其特征是：
-利用设备的主空气压缩机，压缩待蒸馏的所有空气，在达到被认为是高于平均压力的第一高压后，将其分成第一和第二部分;
-至少为被处理的空气流的70%的上述第一部分空气被升压，直到达到第二高压为止;
-在换热管中冷却上述第一部分空气的至少大部分，直至达到一中间温度，在该点，部分空气在平均压力下的第一透平中膨胀，此后，引入平均压力塔，而其余部分被冷却和液化，在膨胀阀中膨胀，然后引入双塔;和
-上述的第二部分空气被冷却和液化，在上述第一高压和上述第二高压之间的至少一个压力下成为至少一个物流，然后在膨胀阀中膨胀，被引入双塔中。
其它的特征是：
-来自第一透平的空气的气态部分在第二透平中膨胀，直达到低压为止，在第二透平中膨胀前，上述的气态部分被部分地预热，在第二透平中鼓入低压塔，（可在冷却后）;
-只利用空气压缩机的一部分级使空气达到第一高压，在该高压下通过除去水分和CO2使空气纯化，利用该压缩机的最后级压缩上述的第一部分空气;
-从压缩机最后级出来的至少部分空气利用连接到第一透平上的一鼓风机升压;
-在上述的第二部分空气导入换热管之前，利用冷冻装置将其预冷。
本发明的另一个目的是提供用于上述方法的一种设备。这种类型的设备包括一主空气压缩机、一用于空气蒸馏的双塔-该双塔包括一在平均压力下操作的平均压力塔和一在低压下操作的低压塔、用于压缩从低压塔底部排出液态氧的泵、使欲蒸馏的空气的一部分达高压的装置和换热管，其特征是：
-上述装置适合于使被蒸馏的所有空气达到被认为是高于平均压力的高压，还包括用于被处理空气流的至少70%的这种空气的第一部分的升压直达到第二高压的装置;
-换热管包括用于冷却上述第一部分空气直到达到中间温度的装置，和进一步冷却和液化上述这种第一部分空气的装置，和用于冷却和液化不升压的空气使在上述第一高压和上述第二高压之间的至少一种压力下成为至少一种物流;和
-该装置包括一膨胀透平，其中吸入侧连接到用于冷却第一高压下的空气的导管上，且在换热管的中点处，它的排气管连接到平均压力塔上。
现参考附图来描述本发明的几个具体实施方案，其中：
-图1是表示本发明的设备的示意图;
-图2是换热图解，由计算得出，相应于图1的设备，是本发明设备操作的第一种模式;在该图中，温度为℃，用x-轴表示，交换的热量用y-轴给出;
-图3是与图2相似的图解，相对应图1设备的另一种操作模式;和
-图4-6是与图1相似的图，它们分别表示本发明设备的三种变体。
图1中示出的空气蒸馏设备主要包括空气压缩机1;通过吸附除去CO2和H2O以纯化压缩空气的装置2，装置2包括二个吸附罐2A、2B，其中一个进行吸附操作，同时另一个是在再生过程中;透平鼓风机组3包括一膨胀透平4和一鼓风或升压机5，其主轴是偶接的，该鼓风机可设置冷冻装置（未示出）;一换热器6，由设备的换热管构成;双蒸馏塔7包括被低压塔9围绕的平均压力塔8，有气化器/冷凝器10建立了塔8的塔顶蒸气（N2）和塔9的塔底液（O2）之间的换热关系;液氧容器11，其底部与液氧泵12连接;液N2容器13，其底部与液N2泵14连接。
该设备的目的是经导管15输送预定高压的气态氧，它的压力在几巴和几十巴之间（在本说明书中，压力为绝对压力）。
为此目的，经导管16从塔9底部排出的液氧贮存在容器11，并通过泵12在高压下以液态导入，然后在此高压下在换热器6的导管17中气化和加热。
用于气化和加热以及用于从双塔排出的其它流体的加热和可能的气化所需要的热量通过在下述条件下的待蒸馏的空气提供的。
待蒸馏的全部空气利用在第一高压下的压缩机1压缩，该第一高压是相当高的高于平均压力塔8的压力，在实践中高于9巴。然后将在18处预冷却并在19处冷却到室温附近的空气在一个吸附罐例如2A中纯化，并分成两部分。
第一部分空气为被处理空气流的至少70%，用升压机5升压到第二高压，这是通过透平4操作实现的。
然后，将第一部分空气导入换热器6的热端，并全部被冷却直到达一中间温度。该空气中的一部分在此温度下继续冷却并在换热器的导管20中液化，此后，在低压塔9的压力下在膨胀阀21中膨胀，并在中间部位引入塔9。剩余的空气在透平4中在平均压力下膨胀，然后经导管22直接送到塔8的底部。
第二部分空气（可用冷冻装置6A（破折线所示）预冷至约-40℃）在第一高压下导入换热管6，冷却、液化直到达到导管20A中的后面的冷端为止，在膨胀阀21A中膨胀后与从膨胀阀21排出的物流混合。
图1示出了双塔设备中通常的导管，所示的该设备是所谓的“顶帽”型，即在低压下生产N2：导管23-25分别用于注入塔9的，其量逐渐增加的膨胀的“富液”（富氧空气）、膨胀的“下部的贫液”（不纯的氮）和膨胀的“上部贫液”（几乎是纯氮），这三种流体分别从塔8的底部、中部和在顶部排出;而导管26用于排出来自塔9顶部的气态氮，导管27用于排空来自下部贫液的注入线的残余气（不纯氮）。低压氮在换热器6的导管28中加热后，经导管29回收，而在换热器导管30中被加热后残余气经导管31排空前用于吸收罐的再生，在这个例子中是罐2B。
图1还示出了一部分的平均压力的液体氮在膨胀阀32中膨胀后，贮存在容器13中，还示出了液体氮和/或液体氧是经导管33（用于氮）和/或导管34（用于氧）供给的。
如上述的FR-A-2，674，011的方法中描述的那样，对升压空气的压力的选择，有如下两种可能性：
当产品氧的压力小于约20巴时，空气的压力是在高氧压下气化期间与氧交换热量的空气的冷凝压力，即在换热图（横座标表示温度，纵座标表示换热量）中两部分空气中的一部分在液化弯曲段G所代表的压力是稍稍在垂直的氧蒸发平坦段P的高压）图2）的右边。在换热管热端的温度的差距用透平4来调节，它的吸入温度以A表示。通过在换热管中在该温度下引入第二部分空气，这种差距被减至最小，即大约为2-3℃，到约+10-+15℃，在图2中中以B段表示。它的这一特征和第二液化段G′（相应于另一部分空气的液化）的存在相结合，就能够改进在FR-A-2，674，011中示出的换热图形。应当注意，这种结果可在不增加装置的情况下取得。冷冻装置6A的存在进一步提高了这种有利的现象。图2的图形相当下述的数值：第一高压：24.5巴;产品氧压力：10巴;第二高压：31巴;第二部分空气：为进料流的28%;在20处的液化部分的相对量：很少;产生的液体：为分离的氧量的40%。
当产品氧的压力高于约20巴时，选择空气的压力在30巴和在气化期间氧中的空气冷凝压力之间。在这种情况下（图3），两部分空气的液化弯曲段相对于氧的气化的平坦段P径向移向左，透平的吸入温度比平坦段P的低。随后，大部分透平化的空气在平均压力下呈液态，由于从设备中经导管33和/或34排出至少一种液态产品（氧和/或氮），设备的冷冻状态达到平衡，换热管热端的温度差距为约3℃。当空气的压为约30巴时，在升高的压力下，排出气态氧产生的约25%的液体就可达到平衡，如果空气压力高于30巴，这种比例还可提高。
图3的图形相应于下述的数值：第一高压：28.5巴;纯化温度：+12℃;第二部分空气：进料流的11%;第二高压：36.4巴;在5.7巴下4的膨胀部分：进料流的77%;20的液化部分：进料空气流的12%;产品氧压力：40巴;液体的生产：分离氧量的35%。
在图4的变体中，来自透平4的空气送入分离罐35。产生的液相直接送入塔8，而气相在换热管中部分加热后，在第二透平36中在低压下膨胀，透平36设有适合的制动器37，然后鼓入塔9。这种变体，由于第二透平的存在而增加了产生的液体，能够在良好的能量条件下生产不纯氧，或以所分离的氧量为代价增加了产生的液体，或仅生产液态氧。
如图5所示，在相同的范围内，在这种气相引入透平36的入口前，使来自分离器35的这种气相升温，直到达到主透平4的温度。在这种情况下，如图所示，在引入塔8以前，有必要将从透平36逸出的空气引入换热管，并将其冷却，直到达到该换热管冷端。
图6示出了另一变体，按照该图，第一高压是主压缩机1的倒数第二级的压力。在该压力下在2处纯化后，空气分成如前述的两部分。第一部分再导入压缩机1的最后级的吸入侧，在高压下从此排出。然后，在38处预冷后，这种空气在5处升压至第二高压，并按上述的处理。第二部分空气直接引入换热管的导管20A。
或者，如破折线表示的，可以除去预冷却器38和鼓风机5之间的空气流，并经导管39送入换热管的另一导管20B中，最后使处于第一和第二压力之间的中压。
图6中已经示出，除了直接来自塔9的顶部的低压气态氮和高压氧外，本设备也可通过从导管33排出的液氮物流在换热管中气化制得加压下的气体氮。氮的气化可通过在导管20、20A、20B中的空气的冷凝进行。
再者，本设备可以生产至少两种不同压力下的气态氧和/或气态氮，如在上述的FR-A-2，674，011中说明的。
在EP-A-5，040，289所述的换热管中冷却和液化前，用一个第二鼓风机（未示出），例如与图5的透平36连接的鼓风机将来自鼓风机5的小部分空气进一步升压。

Claims (10)

1、高压生产气态氧的方法，该方法是在一在平均压力下操作的平均压力塔和一在低压下操作的低压塔的双塔中进行空气蒸馏，该方法包括如下步骤：
利用一主空气压缩机压缩待蒸馏的所有空气，直到达到高于上述平均压力的足够高的第一高压为止，上述的压缩空气分成第一和第二部分；
-将为被处理的空气流的至少70%的第一部分空气升压达高于上述第一高压的第二高压；
-在换热管中将第一部分空气的主要部分冷却，直到达到中间温度，上述冷却过的第一部分空气的一部分在平均压力下于第一透平中膨胀，并将上述膨胀过的部分引入平均压力塔，而上述冷却过的第一部分空气的剩余部分冷却和液化，在膨胀阀中膨胀上述第一部分空气的所说液化过的剩余部分空气；
-冷却和液化所说第二部分空气，产生至少一种至少在上述第一高压和上述第二高压之间的一高压的物流，在膨胀阀中膨胀后，将上述的第二部分空气引入双塔；
泵送在低压塔下部排出的液氧；
在设备的换热管中，通过与空气换热，气化泵送的液氧。
2、权利要求1的方法，包括在第二透平中膨胀来自第一透平的空气的气态部分，在第二透平将这部分气体膨胀前，使其加热，并从第二透平排出后鼓入低压塔。
3、权利要求1的方法，其中主压缩机有一组级，包括至少一初始级和一最后级，利用主空气压缩机的至少一个上述的初始级使空气达到第一高压，而在此第一高压下从空气中除去CO2和水，并且上述的第一部分空气利用上述的主空气压缩机的上述的至少一个最终级压缩。
4、权利要求3的方法，其中将从上述主空气压缩机的上述至少一最终级排出的空气流的至少一部分用连接到第一透平上的鼓风机升压。
5、权利要求1的方法，其中上述第二部分空气在引入换热管前，利用冷冻装置预冷却。
6、高压生产氧气的设备，该类型的设备包括一主空气压缩机、一用于蒸馏空气包括在平均压力下操作的平均压力塔和在一低压下操作的低压塔的双塔、用于压缩从低压塔底部排出的液氧的泵、使欲蒸馏的部分空气达一高压空气的装置，和换热管，其特征是：
-上述装置适宜于使被蒸馏的所有空气达到高于平均压力相应高的第一高压并包括在上述第一高压下将空气分离成第一部分和第二部分的装置、被处理的空气流的至少70%的上述第一部分空气升压的装置，该装置将第一部分空气的压力升达高于上述第一高压的第二高压;
-换热管包括用于将上述第一部分空气冷却降到中温度;使其进一步冷却并液化的装置;用于冷却和液化在至少一种压力的至少一种不升压空气的装置，上述的至少一种压力是在上述第一高压和上述第二高压之间;和
-包括有吸入侧和排气侧的第一透平设备，上述的吸入侧连接到用于冷却第一高压空气的导管上，它在换热管的中间部位，上述的排气侧连接到平均压力塔上。
7、权利要求6的设备，其中包括用于将从第一透平排出的空气流的至少一部分膨胀到低压的第二透平。
8、权利要求6的设备，其中上述的第二部分空气是来自主空气压缩机的中间级，在通过除去水和CO2纯化后，第一部分空气再引入该压缩机。
9、权利要求8的设备，包括吸入侧连接到第一透平上的鼓风机，透平的其吸入侧连接到主空气压缩机的最后级的输入端上。
10、权利要求6的设备，包括用于换热管的上游的上述第二部分空气的预冷的冷冻装置。
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CA2115399A1 (fr) 1994-08-13
FR2701553A1 (fr) 1994-08-19
DE69414282T2 (de) 1999-06-17
CA2115399C (fr) 2005-04-26
AU660385B2 (en) 1995-06-22
EP0611218A1 (fr) 1994-08-17
AU5506094A (en) 1994-08-18
DE69414282T3 (de) 2003-03-20
JPH06241650A (ja) 1994-09-02
FR2701553B1 (fr) 1995-04-28
EP0611218B2 (fr) 2002-08-07
EP0611218B1 (fr) 1998-11-04
ES2124856T3 (es) 1999-02-16
ES2124856T5 (es) 2003-03-01
DE69414282D1 (de) 1998-12-10
ZA94968B (en) 1994-08-24
US5426947A (en) 1995-06-27

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