CN1081782C - 在压力下生产气态氧的方法和装置 - Google Patents

在压力下生产气态氧的方法和装置 Download PDF

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CN1081782C
CN1081782C CN95107033A CN95107033A CN1081782C CN 1081782 C CN1081782 C CN 1081782C CN 95107033 A CN95107033 A CN 95107033A CN 95107033 A CN95107033 A CN 95107033A CN 1081782 C CN1081782 C CN 1081782C
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M·格里尼尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

在“泵增压”型方法中，将空气分成数物流。将第一物流压缩到中压、冷却并送入双蒸馏塔(7)。将第二物流压缩到约25巴以上，但低于由液态氧在压力下汽化产生的冷凝压力，然后冷却到中间温度，在此温度下，一部分空气继续冷却并液化(在20A中)，然后膨胀(在21A中)，并直接送入双塔，而其余的空气通过透平(在4中)。应用于生产氧的大型装置。

Description

在压力下生产气态氧的方法和装置
本发明涉及一种在压力下生产气态氧的方法。在该法中，空气在有双蒸馏塔的装置中蒸馏。该装置包括一座在称为中压的压力下操作的中压塔、一座在称为低压的压力下操作的低压塔以及一套使要蒸馏的空气与从双塔中取出的产品进行热交换的热交换器；液态氧从低压塔取出；将其加压至至少为13巴的氧气汽化压力，使其汽化，并在这一汽化压力下通过与在冷却过程中的要蒸馏的空气的热交换被加热。
在本说明书中，所指的压力是绝对压力。而且，“冷凝”和“汽化”应理解为既是真正的冷凝或汽化，也是假冷凝或假汽化，取决于压力是亚临界压力或是超临界压力。
上述方法称为“泵增压”法，其优点是取消或减小所需的气态氧压缩机，这样的压缩机是昂贵的机械，其可靠性有严重问题，而效率通常不高。
本发明旨在提供一种“泵增压”法，它对操作参数的控制有很大的灵活性，从比能耗和液体产品生产率的观点看，它特别适合于大型装置，也就是说每天生产至少700吨氧的装置。
为此，本发明的目的是生产上述类型气态氧的方法，其特征在于：
——将要蒸馏的第一部分空气压缩到接近中压的第一压力，这部分空气在热交换器中冷却直到接近其露点，然后送入双塔；
——将要蒸馏的第二部分空气压缩到高空气压力，特别是至少约25巴，该压力低于与在所述的氧汽化压力下汽化过程中的氧进行热交换的空气的冷凝压力，该空气被冷凝，其中一部分被液化，然后该空气在送入双塔以前进行膨胀，而另一部分在高空气压力下的空气在中间冷却温度下从热交换器中取出，并在膨胀透平中膨胀到中压，然后送入中压塔；以及
——至少一种液体产物从装置中取出。
本发明的方法可能有以下一个或多个特征：
——将要蒸馏的第三部分空气压缩到所述的第一压力和高空气压力之间的中间压力，冷却，液化，膨胀，然后送入双塔；
——将所述的第二部分空气压缩到中间空气压力，仅进行部分冷却，然后用冷鼓风机增压，再送入热交换器，并冷却到所述的中间温度，在这一温度下，该空气再次从热交换器中取出，在所述的膨胀透平中膨胀到中压，膨胀透平与冷鼓风机相连，然后将空气送入双塔；
——将第三部分空气中的一部分部分冷却后，在与使所述的第二部分空气增压的鼓风机相连的第二透平中膨胀到中压，然后送入中压塔；
——在第三中间冷却温度下将一部分在第一压力下的空气从热交换器中取出，在送入低压塔中部以前在鼓风机透平中膨胀到低压；
——所述的氧汽化压力基本上是出口压力。
本发明的另一目的是一套使用上面确定的方法生产气态氧的装置。该装置包括双空气蒸馏塔，它有一座在称为中压的压力下操作的中压塔和一座在称为低压的压力下操作的低压塔；一套热交换器，用于使要蒸馏的空气与来自双塔的产品进行热交换；从低压塔取出液态氧的设备；使该液态氧的氧汽化压力至少为约13巴的设备。热交换器包括使在所述的汽化压力下的液态氧与处于冷却过程中的要蒸馏的空气进行热交换的设备。其特征在于，装置包括：
——用于将第一部分要蒸馏的空气压缩到接近中压的第一压力的第一压缩设备，以及一端与该第一压缩设备相连而另一端与双塔相连的热交换器管线；
——用于将第二部分要蒸馏的空气压缩到高空气压力，特别是至少约25巴的第二压缩设备，该压力低于与在所述的氧汽化压力下汽化的氧进行热交换的空气的冷凝压力；
——热交换器包括用于使所述的第二部分空气冷却到中间温度和用于使第二部分空气中的一部分进一步冷却和液化的管线，以及该装置包括用于该液化的空气部分膨胀的设备，它与双塔相连；
——一台膨胀透平，其吸入管与高压空气管线相连，而排出管与双塔相连；以及
——从装置取出至少一种液体产品的设备。
该装置特别可能包括一台有n级的单一空气压缩机，一定数目p级构成所述的第一压缩设备，p＜n，它与所述的第二压缩设备一起构成了整个压缩机。
现在参照附图描述实施本发明的一些例子。附图中，图1-图3分别表示按照本发明生产氧的三套装置。
在图1中所示的空气蒸馏装置主要包括：一台空气压缩机1；一套用于经压缩的空气吸附脱水和脱CO2的纯化设备，该设备有两个吸附罐2A、2B，其中一个处于吸附操作而另一个处于再生过程中；一台鼓风机透平3，包括膨胀透平4和鼓风机或增压机5，它们的轴相连，鼓风机还可装有冷凝器(未表示出)；一套由装置的热交换管线构成的热交换器6；一双蒸馏塔7，包括一座中压塔8，其上有一低压塔9，冷凝汽化器10使塔8的塔顶蒸汽(氮气)与塔9的塔釜液体(氧)进行热交换；一液态氧贮罐11，其底部与液态氧泵12相连；一液态氮贮罐13，其底部与液态氮泵14相连。
该装置主要用于通过管线15提供预定高压的气态氧，该压力可在约13巴至几十巴之间。该装置涉及到生产大量的气态气，至少约700吨/天，并能达到每天数千吨。
为此，从塔9釜底通过管线16取出的液态氧贮存在贮罐11中。从该贮罐取出的氧流通过泵12产生液态高压，然后在此高压下在热交换器6的管线17中汽化和加热。
通过要蒸馏的空气在以下条件下为该汽化和加热提供所需的热量，也为从双塔中取出的其他液体的加热，有时还可为汽化提供所需的热量。
压缩机1是有n级的多级压缩机。进入的所有常压空气通过前p级压缩到中压，即塔8的操作压力，然后在18中预冷却，后在19中冷却到接近常温，在吸附罐之一(如2A)中纯化，然后分成两部分。
第一部分在中压下的空气，如为被处理的空气注流约40％在热交换器6的管线20中从热端流到冷端被冷却，一直到其温度接近露点，然后将它直接送入塔8的塔釜。将在2A中纯化的其余空气送回压缩机1的(p+1)级入口，并通过以后的各级压缩到第一高空气压力，该压力明显高于塔8的中压，实践中高于9巴。
如此压缩和在19A中预冷却的空气再次分成两气流。
第一气流为至少45％处理的空气气流，用由透平4驱动的增压机5增压到第二高空气压力。这第二高空气压力在约25巴至通过在高氧气压力下氧汽化得到的空气冷凝压力之间。
然后将第一空气流送入热交换器6的热端，并全部冷却到中间温度。在这一温度下，一部分空气继续冷却，并在热交换器的管线20A中液化，然后一部分在膨胀阀21中膨胀到低压，而另一部分在膨胀阀21A中膨胀到中压，并分别送入塔9的中部和送入塔8的下部。在中间温度下其余的空气在透平4中膨胀到中压，然后通过管线22直接送到塔8的底部。
将在第一高空气压力下的第二气流送入热交换器6，在管线20B中一直到热交换器的冷端为止被冷却和液化，在膨胀阀21B中膨胀，然后与来自膨胀阀21A的气流合并。
在图1中还可看见的是双塔装置常见的管线，通常所说的尖塔(minaret)，也就是说对于低压氮生产：管线23-25在不同的高度，分别用于送入膨胀后的“富液”(富氧的空气)、膨胀后的“低贫液”(杂质氮)和膨胀后的“高贫液”(特别纯氮)。这三个物流分别从塔8的底部、中部和顶部取出，管线26用于取出离开塔9顶部的气态氮，管线27用于除去离开低贫液注入高度的残留气体(杂质氮)。低压氮在热交换器6的管线28中被加热，然后通过管线29回收，而残留气体在热交换器的管线30中加热后，在通过管线31排放前，用于再生吸收罐，在所研究的实例中为罐2B。
在图1中还可看出，一部分中压液态氮在膨胀阀32中膨胀后贮存在贮罐13中，并可看出通过管线33(在氮的情况下)和/或管线34(在氧的情况下)提供液态氮和/或液态氧。而且，除了直接来自塔9塔顶的低压气态氮以及高压气态氧外，该装置还生产在压力下的气态氮，它通过取自管线33的液态氮经管线35在热交换器中汽化来得到。这一氮的汽化特别是可通过管线20A或20B中的空气的泠凝来实现。
正如在其他专利说明书中的描述的“泵增压”法和有“偏置平台”(offset plateaus)的泵增压法，也就是说在该法中，如在本发明中，为氧提供大部分汽化热的空气被冷凝到该氧的汽化温度以下(如见法国专利申请书91-02917、91-15935、92-02462、92-07662和93-04274)，装置的致冷平衡是平衡的，热交换器热端的温差为约3℃，通过管线33和/或34从装置取出至少一种液体形式的产品(氧和/或氮)。
在上述方法中，使一部分进入的空气仅压缩到中压的事实减少了需要从装置中取出的液体数量。这一点在大型装置中是很有利的。在大型装置中，用背景技术的方法所取出的液体数量是很大的。而且，必须取出较少量液体的事实与这些大型装置的操作条件完全不矛盾，通常它也必须产生一定数量的液体。
此外，计算表明，上述方法有十分有利的氧生产比能耗。
图2所示的装置用于生产高压(如约40巴)气态氧。它主要有两台空气压缩机41和42、一套用于吸附纯化的设备43、双蒸馏塔44(由在约6巴下操作的中压塔45和叠在它上面的、在稍高于1巴压力下操作的低压塔组成)、一台热交换器47、一台过冷却器48、一台液态氧泵49、一台冷鼓风机50、一台其叶轮安装在与冷鼓风机相同轴上的第一透平51以及一台用适宜制动装置53如振荡器制动的第二透平52。
在图2中可看出的是双塔中的常规管线，即管线54，用于将塔45的塔釜中收集的“富液“(富氧的空气)在48中过冷并在膨胀阀55中膨胀到低压后提送到塔46的中部；管线56，用于将从塔45顶部取出的“贫液”(实际上是纯氮)在48中过冷并在膨胀阀57中膨胀到低压后提送到塔46的顶部；以及管线58，用于取出装置中的残留气W形成的杂质氮，从塔46顶部离开的这条管线通过过冷却器48，然后与用于加热热交换器47的氮的管线59连接。如此加热到常温后，杂质氮通过管线60从装置中排出。
泵49在大约1巴下从塔46塔釜取出液体氧，使它达到所需的出口压力，并将它送入管线61，以便在热交换器中氧的加热汽化。
要蒸馏的空气用压缩机41压缩到中压，然后在43中纯化脱水和脱CO2，再分成两流。
第一空气流在热交换器47的管线62中直接冷却。在温度T1下(该温度相当低，但高于热交换器的冷端温度)，该空气流的一部分从热交换器中取出，在透平52中膨胀到低压，然后通过管线63送到塔46的中部。其余的中压空气继续冷却，一直到热交换器的冷端，在那里其温度接近露点，然后将它送入塔45的塔釜。
来自设备43的其余空气用压缩机42压缩到第一高压，如16.5巴，然后进入热交换器的空气冷却管线64。
在中间温度T2下(它比常温低，但明显高于T1和接近氧的汽化温度)，该空气的一部分通过管线65从热交换器中取出，送到冷鼓风机50的吸入管。冷鼓风机50使这一空气达到23巴的高压，然后将如此增压的空气在高于T2的温度T3下通过管线66送回热交换器，继续在热交换器的增压空气管线67中冷却。一部分通过管线67输送的空气在第二中间温度T4(它低于T2而高于T1)下再次从热交换器中取出，并在透平51中膨胀到中压(6巴)。从这一透平出来的空气被送到塔45的塔釜。通过管线67输送的其余空气继续冷却，一直到热交换器的冷端，同时被液化和过冷。然后它在膨胀阀68中膨胀到中压，并送入塔45塔釜上方几块塔板处。同样，通过管线64输送的、未通过管线65取出的空气被冷却一直到热交换器的冷端，然后在膨胀阀69中膨胀到中压，并送入塔45塔釜上方几块塔板处。
正如在上述申请书FR92 02462中说明的，至少一部分在第一高压下的空气从接近氧汽化平稳段的中间温度T2压缩到温度T3，在这两个温度之间送入热交换器，一定数量的热量相当大地抵偿了由这一汽化产生的过量的冷量。应当指出，在T3和T2之间氧与所有在16.5巴下的空气进行热交换，同时空气增压到23巴。如此有可能得到热交换图(热函为纵座标，温度为横座标)，该图是很有帮助的，在热交换器的热端，有小的温差，约2-3℃。
确保这一压缩的鼓风机50是用透平51驱动的，结果是不需要外加能量。考虑到机械损失，由这一透平产生的冷量稍大于压缩的热量，过量的冷量有助于使装置保持冷却。为保持冷却所需的其余的负卡路里由透平52提供，或者作为替代方法，如果要生产的氧必须有高的纯度，通过空气或氮气在透平中以传统的方式膨胀到中压。
在这里保持了通过使用冷鼓风机50确保的很高的能效，有另外的优点，如上所述，在这种情况下有较少的或甚至没有液体输出，另一优点是简化了注入透平52的进料。
该装置也能生产在以下压力下的氧，该压力足以低到在该法最高空气压力下通过空气的冷凝使氧汽化。这一氧压例如可低于8巴，例如，将降低纯度的液态氧压缩到低于8巴的中间压力的第二泵70已用虚线示于图2。这一氧通过用鼓风机50增压的相应部分空气的冷凝而汽化，它需要仅提供抵偿由于高压氧汽化产生的过量冷量所需的热量。
在图2中还用虚线示出，中压液态氮泵71使从塔45取出的氮达到中间压力，这一压力足以低到在最高的过程压力下即23巴下通过空气的冷凝使氮汽化。
图2还示出管线72，用于从塔46的塔釜取出液态氧产品，以及管线72A，用于来自塔45顶部的液态氮的生产。
图3中的装置是图2装置的一替代形式。在这一替代形式中，一部分来自压缩机42的空气用热鼓风机73，增压，在47中冷却到温度T2，再次用冷鼓风机50增压，在高于T2的温度T3下再送入热交换器，然后象以前一样分成两个由温度T4开始的物流。来自压缩机42的其余空气在热交换器47的另一管线74中冷却到温度T5，它处于温度T4和T1之间，在这一温度下，一部分空气从热交换器中取出，然后在与鼓风机73相连的另一透平75中膨胀到中压，再送入塔45的塔釜。由管线74输送的其余空气继续冷却一直到热交换器的冷端，在这里它被液化和过冷，然后在膨胀阀76中膨胀到中压，再送入塔45的下部。
应当理解，本发明与许多在“泵增压”和偏置平台型的压力下生产气态氧的装置，特别是在上述专利申请书中描述的装置的替代形式是不矛盾的。
从能量的观点看，当氧汽化压力大于约20巴时，本发明是特别有利的。

Claims (12)

1.一种在压力下生产气态氧的方法，其中空气在有双蒸馏塔(7，44)的装置中进行蒸馏，该装置包括一座在称为中压的压力下操作的中压塔(8；45)、一座在称为低压的压力下操作的低压塔(9；46)以及一套使要蒸馏的空气与从双塔中取出的产品进行热交换的热交换器(6；47)；液态氧从低压塔取出；将其加压至至少为约13巴的氧气气化压力，使其汽化，并在这一汽化压力下通过与在冷却过程中要蒸馏的空气的热交换被加热，其特征在于：
-将要蒸馏的第一部分空气压缩(在1；41中)到接近中压的第一压力，这部分空气在热交换器(6，47)中冷却直到接近其露点，然后送入双塔(7；44)；
-将要蒸馏的第二部分空气压缩(在1、5；41、42、50、；41、42、73、50中)到高空气压力，该压力低于与在所述的氧汽化压力下汽化过程中的氧进行热交换的空气的冷凝压力，该空气被冷凝，其中一部分被液化，然后该空气在送入双塔以前进行膨胀(在21、21A；68)中，而另一部分在高压空气压力下的空气在中间冷却温度下从热交换器(6；47)中取出，并在第一膨胀透平(4；51)中膨胀到中压，然后送入双塔(7；44)；以及
-至少一种液体产物从装置中取出(在33、34、72、72A)。
2.根据权利要求1的方法，其特征在于，将要蒸馏的第三部分空气压缩(在1；1、42中)到所述的第一压力和高空气压力之间的中间压力，冷却，液化(在20B；64；74中)，膨胀(在21B；69；76中)，然后送入双塔(7；44)。
3.根据权利要求1或2的方法，其特征在于，将所述的第二部分空气压缩(在42；42、73中)到中间空气压力，仅部分被冷却，然后用冷鼓风机(在50中)增压，再送入热交换器(47)，并冷却到所述的中间温度，在这一温度下，该空气再次从热交换器中取出，在所述的膨胀透平(51)中膨胀到中压，膨胀透平与冷鼓风机相连，然后将空气送入双塔(44)。
4.根据权利要求2的方法，其特征在于，将所述的第二部分空气压缩(在42；42、73中)到中间空气压力，仅部分被冷却，然后用冷鼓风机(在50中)增压，再送入热交换器(47)，并冷却到所述的中间温度，在这一温度下，该空气再次从热交换器中取出，在所述的膨胀透平(51)中膨胀到中压，膨胀透平与冷鼓风机相连，然后将空气送入双塔(44)；将第三部分空气中的一部分部分冷却后，在与使所述的第二部分空气增压的鼓风机(73)相连的第二透平(75)中膨胀到中压，然后送入中压塔(45)。
5.根据权利要求4的方法，其特征在于，在第三中间冷却温度下，将一部分在第一压力下的空气从热交换器(47)中取出，在送入低压塔(46)中部以前在鼓风机透平(52)中膨胀到低压。
6.根据权利要求1的方法，其特征在于，所述的氧汽化压力基本上是出口压力。
7.一套在压力下生产气态氧的装置，它包括一座双空气蒸馏塔(7；44)，它有一在称为中压的压力下操作的中压塔(8；45)和一在称为低压的压力下操作的低压塔(9；46)；一套热交换器(6.47)，用于使要蒸馏的空气与来自双塔的产品进行热交换；从低压塔取出液态氧的设备；使该液态氧的汽化压力至少为约13巴的设备(12，49)，热交换器包括使在所述的汽化压力下的液态氧与处于冷却过程中的要蒸馏的空气进行热交换的设备，其特征在于，装置包括：
-用于将第一部分要蒸馏的空气压缩到接近中压的第一压力的第一压缩设备(1；41)，以及一端与该第一压缩设备相连，而另一端与双塔(7，44)相连的热交换器管线(20；62)；
-用于将第二部分要蒸馏的空气压缩到高空气压力，该压力低于与在所述的氧汽化压力下汽化的氧进行热交换的空气的冷凝压力；
-热交换器包括用于使所述的第二部分空气冷却到中间温度和用于使第二部分空气中的一部分进一步冷却和液化的管线(20A；64)，以及该装置包括用于该液化的空气部分膨胀的设备(21A；68、69)，它与双塔相连；
-一台第一膨胀透平(4、75)，其吸入管与高压空气管线(74)相连，而排出管与双塔(7；44)相连；以及
-从装置取出至少一种液体产品的设备(72；72A)。
8.根据权利要求7的装置，其特征在于，它包括用于将第三部分要蒸馏的空气压缩到中间压力的设备(1；1、42)，中间压力在所述的第一和高空气压力之间；热交换器(6；47)包括用于冷却和液化该第三部分空气的管线(20B；64、74)和将这些管线的冷端连接到双塔(7，44)并装有膨胀阀(21B；69；76)的管线。
9.根据权利要求7或8的装置，其特征在于，它包括一台有n级的单一空气压缩机(1)，一定数量p级构成所述的第一压缩设备，p＜n，它与所述的第二压缩设备一起构成了整个压缩机。
10.根据权利要求7或8的装置，其特征在于，第二压缩设备(42，50)包括一台压缩机，其出口管连接到热交换器(47)的热端，以及一台鼓风机(50)，其吸入管和出口管连接到热交换器的中部。
11.根据权利要求8的装置，其特征在于，第二压缩设备(42，50)包括一台压缩机，其出口管连接到热交换器(47)的热端，以及一台鼓风机(50)，其吸入管和出口管连接到热交换器的中部，第二压缩设备还包括一台鼓风机(73)，用于使所述的第二部分空气增压，并与用于使一部分所述的第三部分空气膨胀的第二透平(75)相连。
12.根据权利要求10的装置，其特征在于，冷鼓风机(50)与所述的第一透平(51)相连，该装置包括一台鼓风透平(52)，一部分在第一压力下的空气为进料，出口管连接到低压塔(46)。
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