CN1168463A - 生产高压氧的方法及设备 - Google Patents

生产高压氧的方法及设备 Download PDF

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CN1168463A
CN1168463A CN97110054A CN97110054A CN1168463A CN 1168463 A CN1168463 A CN 1168463A CN 97110054 A CN97110054 A CN 97110054A CN 97110054 A CN97110054 A CN 97110054A CN 1168463 A CN1168463 A CN 1168463A
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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

本方法是一种通过压缩从低压塔(11)的壳体中抽出的液氧来在理想的高压下直接生成气态氧的方法。待蒸馏的空气被分成三股流：双蒸馏塔(1)的中压流，约高于60巴的高压流，以及部分冷却后在透平机(8)中膨胀到中压的过渡压力流。所选择的过渡压力应使待进入透平机处理的空气在透平机叶轮的入口处接近其自身的露点温度。同时从设备中(在24处)抽出液体产品。应用上述方法的设备可在大于30巴的压力下生产大量气态氧。

Description

生产高压氧的方法及设备
本发明涉及一种至少在大约30巴的高压下生产气体的方法，用这种方法，空气在一个双馏塔设备中蒸馏，此双馏塔设备包括一个在低压下运行的蒸馏塔和一个在中压下运行的蒸馏塔，将从设备的一个塔中抽出的液体增压，压缩的液体在焊接板式换热器中与冷却和/或液化过程中的空气进行热交换而被蒸发，最后从设备中至少抽出一种液态产品。
本发明特别适用于大量高压气态氧的生产，如典型的500吨/日以上的产量。
本发明所述压力为绝对压力。
上述的几个过程，如“增压过程”已提出过了，本发明的目的是提出一种相同类型的方法，从单位能量消耗的观点来看，该方法具有特定的优点。
为此本发明的任务是提出一种上述类型的方法，其特征在于将待蒸馏的空气分成三股流：
—第一股中压空气流被冷却到其自身的露点附近，然后进入中压塔；
—第二股高压空气流的压力约大于60巴，它被冷却和液化，然后在膨胀后进入双塔；以及
—第三股为过渡压力的空气流，这第三股空气流的至少一部分于进入中压塔之前在透平机内以中间冷却温度膨胀至中压，所选择的过渡压力应使空气在透平机叶轮的入口处接近其露点温度。
该方法可以具有一个或更多的下述特性：
—所述的液体产物至少部分是从与双塔相连的一个用于氧/氩分离的辅助塔中生产的液态氩；
—所述全部液体产品是液态氩；
—只借助透平机提供的机械能将所述第二空气流从过渡压力压缩至高压；
—所述中间温度接近于较高氧压下的氧的蒸发温度；
—氧的高压接近于40巴，并且从设备中抽出的液态产品的流量基本上由DL＝-0.22P+22限定，其中DL是抽出的液体产品的流量与生产的氧的总流量的百分比，而P是以巴表示的空气的绝对高压；
—抽出的液体产品的流量大约占生产的氧的总流量的2％到12％之间；
—所述第二和第三空气流分别大约为待蒸馏的空气总流量的20-25％和10-20％。
本发明的另一个目的是提供一种实现上述方法的设备。这种设备用于在至少约30巴的氧高压下生产气态氧，这种设备包括：一个含有一个以低压运行的塔和一个以中压运行的塔的双空气蒸馏塔、一个用于压缩从设备的一个塔中抽出的液体的泵、压缩进入的空气的装置、一个用于使待蒸馏的空气和压缩液体进行热交换的焊接板式换热器以及用来从设备中抽出至少一种液体产品的管子，其特征在于压缩装置包括分别以空气的中压、过渡压力和高压形成三股空气流的装置，在于热交换器包括从其热端到冷端冷却中压空气的通路、过渡压力下的空气的部分冷却通路和从其热端到冷端冷却高压空气的通路，其特征还在于该设备还包括一个至少将一部分在过渡压力下的部分冷却空气膨胀到中压的透平机和一个与双塔相连生产液态氩的塔。
在该设备的一个实施例中，该设备包括一个通过蒸发从低压塔的贮槽中抽出的液氧来使从中压塔的贮槽中抽出的液体过冷的附加换热器。
本发明应用的实施例将参照附图进行描述。
—图1概要地图示了本发明用于生产气态氧的设备；
—图2是相应热交换的曲线图；
—图3是表示在最经济的状态下，设备中液体氧的输出随氧高压变化的函数曲线图；
—图4概要地图示了图1所示设备的另一个替换形式。
图1所示设备是用于在至少约30巴的压力下生产气态氧的设备。它主要包括一个双馏塔1、至少由一个焊接板式换热器体构成的一个主热交换段2、一个过冷器3、一个空气压缩机4、一个用于去除空气中的水份和CO2的空气吸附净化装置5、第一空气增压器6、第二空气增压器7、一个膨胀透平机8和液氧泵9。按照常规方式，双塔由一个中压塔10和一个位于该中压塔上的低压塔11组成，其中中压塔10的工作压力大约为5-6巴，低压塔11的工作压力稍大于大气压，且在低压塔的壳体内带有一个蒸发-冷凝器12，它使来自低压塔壳体内的液氧与来自中压塔顶部的氮进行热交换。
在操作中，待蒸馏的空气全部由压缩机4压缩到中压并在5中净化，而后被分成二股流体。
中压的第一股流体在热交换段20的通路13中进行冷却，此流体从通路13的热端到达其冷端。该中压空气以接近自身露点的温度离开热交换段，并进入中压塔10的底部。
离开装置5的其余空气在6中增压至过渡压力，并再次被分成两股流体。
此过渡压力下的第一股流体在热交换段的通路14中冷却到一中间温度T1。该股流的一部分任选地继续冷却，并在热交换段的冷端被液化，然后在膨胀阀15中膨胀至中压并又分成两股流体：一股流输送到塔10的底部，另一股流在3中过冷，在膨胀阀16中膨胀到低压，然后输送入塔11。第一股流体的其余部分以中间温度T1从热交换段抽出，并在透平机8中膨胀至中压，然后进入塔10的底部。
第二增压的空气流在第二增压器7中再次被增压达到约60-80巴的第二高压，然后在热交换段的通路17冷却并在通路的冷端液化。如此得到的液体在膨胀阀18中膨胀并与从膨胀阀15中产生的液化流体混合。
从塔11的贮槽中抽出的液氧靠泵9达到理想的输出高压，然后在经一输出管19从设备中排出之前，此液氧在热交换段的通路18中被蒸发、加热。
此外，图1还示出了双塔设备中常用的管路和辅助装置：将集聚在塔10壳体内的“高品位液体”(富氧空气)向上返回到塔11中的带膨胀阀21的管路20、将从塔10的顶部抽出的“低品位液体”(近于纯氮)向上返回到塔11顶部的带有膨胀阀23的管路22，以及一些下述管路：安装在塔11壳体上的液氧输出管24、接在管路22上并带有膨胀阀26的液氮输出管25和安装在塔11顶部从设备中抽出含有残余气体的非纯氮的管路27。该非纯氮在经管路29被排出之前先在过冷器3中然后在热交换段的通路28中进行再加热。在过冷器3中使产生于膨胀阀15和18的液态空气、低品位液体和高品位液过冷，对高品位液体来说，约过冷2℃。
为了得到尽可能低的单位能量消耗(此单位能量是指在高压下生产单位数量的气态氧所需的能量)，热交换段2的热交换曲线的温差应尽可能的小，以便接近可逆换热条件。特别是在图2的曲线中，焓H作为横坐标，温度作纵坐标，在热交换段的热端、冷端以及氧蒸发的平稳阶段30的起点处，被冷却的空气(曲线C1)和被加热的产品(曲线C2)之间的温差必须尽可能小。
在一定条件下，通过模拟计算，当平稳阶段30起点处有一最小温差1.5℃时，则能够得到接近于5℃的平均温度差，适用条件如下：
—在考虑焊接板式换热器2的制作技术的情况下，尽可能地选择较高的空气高压。这个高压典型地约在60-80巴之间。
—中间温度T1，即透平机8的进口温度，它接近于氧的蒸发温度，最好比该蒸发温度高出1℃。
—选择过渡压力，以使由透平机处理的空气在透平机叶轮的入口处接近自身的露点温度。
如已知的那样，低温透平机叶轮后接有一入口分配器。该分配器导致第一次焓的释放或下降，这正是此透平机的特性。上述第三个条件使人们能易于确定过渡压力，此压力即是空气必须进入透平机以便在叶轮入口处达到其露点附近温度所具有的压力。该过渡压力大约在30-40巴之间。
此外，在24处必须抽出一定流量的液体，这样相应地减少了须在热交换段进行加热的产品量，并该液体的流量是氧高压和空气高压的函数。图3示出在氧高压为40巴下，当空气高压P从稍高于60巴的压力变化到80巴时，最经济的液体流量按照：DL＝-0.22P+22的规律基本上直线下降，其中，DL是用百分比表示的抽出的液氧流量与所生成的氧的总流量的比值。
如所看到的那样，根据计算结果，如果能选择空气高压显著大于80巴并大约为100巴时，流量DL会趋于零。
在上述例子中，透平机8产生的机械能被回收以便驱动增压器7，但增压器也可有一外部驱动源。在另一种替代形式中，如果使透平机8与增压器匹配使用，以便简化设备，则过渡压力和中间温度T1必须升高，计算表明这会导致流量DL和单位能量的增加。
作为例子，过渡压力和高压力下的空气流能分别占所处理的空气流量的约20％和约25％。
现回到图3，可以发现，当在40巴的压力下生产氧时，在空气高压接近80巴的情况下，流量DL约为4.5％。那么，这一百分比是大气中氩与氧的比值。因此，如图4所示，为双馏塔加一个分离氩/氧的辅助塔31，并在辅助塔31后联接一个去除最后的微量氧的装置31A，并在31A后再接脱氮的装置31B，则最经济地抽出的液体产品能够只是纯液氩从设备中的输出。
在提出这一特有的先进技术之前，由于设备比较复杂，上述过程主要应用在具有较大生产能力的设备中，在这些设备中，单位能量是一个很重要的指标，并且这些设备恰好为附加一个氩生成塔提供了充分的理由。
在图4中，以常规的方法，塔1的壳体是由两根管子32(送入)和33(返回)连接到塔11的“氩支路连接部分”的，同时氩生产塔的顶部装有一个冷凝器34，在该冷凝器中蒸发由35处膨胀至接近大气压的高品位液体，该液体然后经管道36返回塔11中。经管道37从塔31顶部抽出的不纯气态氩先在31A然后在31B中进行净化，然后将纯氩以液态形式经输出管37A从设备中抽出。
如图4所示，以另一种替换形式，在于21和可任选的35处进行膨胀之前，高品位液体的过冷可在辅助热交换器38中通过蒸发从塔11的贮槽中抽出的液氧来实现。这样使在利用“泵”法过程中循环的大量高品位液体能够过冷4-5℃，因此提高了氧和相应氩的分离效率。
在如图1和4中虚线所示的另一方式中，该设备能够另外产生具有一定压力的气态氮，该氮以液态从管道22中抽出，靠泵39加到一理想的压力，在热交换段2的通道40中蒸发加热，然后经输出管41抽出。
很明显，在本发明的方法中，全部或部分抽出液体也可以是液氮(管25)。
加压后蒸发的液体可以是氧、氮或氩。

Claims (13)

1.在至少约30巴的高压下生产气体的方法，用这种方法，空气在具有双馏塔(1)的设备中蒸馏，双馏塔(1)包括一个低压运行的塔(11)和一个中压运行的塔(10)，从设备中的一个塔(11)中抽出的液体被加压(在9处)，压缩的液体在焊接板式热交换器(2)中与冷却和/或液化过程中的空气进行热交换而蒸发，并且至少从设备中(在24，25；37A处)抽出一种液体产物，其特征在于待蒸馏的空气被分成三股流体：
—第一股中压空气流被冷却到其自身露点温度附近，然后进入中压塔(10)；
—第二股高压空气流的压力约高于60巴，它被冷却和液化(在17处)，然后在膨胀(在18处)后进入双塔(1)；以及
—第三股流为过渡压力空气流，该股流的至少一部分在进入中压塔(10)之前，在透平机(6)内以中间冷却温度膨胀至中压，所选择过渡压力应使空气在透平机叶轮的进口处接近其自身的露点温度。
2.根据权利要求1所述的方法，其特征在于所述液体产品至少部分是从一个与双塔(1)相连的用于氧/氩分离的辅助塔(31)中生产的液氩。
3.根据权利要求2所述的方法，其特征在于全部液体产品是液氩。
4.根据权利要求1至3之一所述的方法，其特征在于所述第二股空气流从过渡压力向高压的压缩只依靠由透平机(6)提供的机械能完成。
5.根据权利要求1至3之一所述的方法，其特征在于所述的中间温度接近于高压液体的蒸发温度。
6.根据权利要求1至3之一或5所述的方法，其特征在于高压接近于40巴，并且从设备中抽出的液体产品的流量基本上由：
DL＝-0.22P+22限定，其中，DL是以百分比表示的抽出的液体流量与生产的氧总流量的比值，而P是以绝对压力巴表示的空气高压。
7.根据权利要求1至6之一所述的方法，其特征在于抽出的液体产品的流量大约占生产的氧的总流量的2％和12％之间。
8.根据权利要求1至7之一所述的方法，其特征在于所述第二和第三股空气流分别占待蒸馏的空气总流量的约20％-25％和约10％-30％。
9.根据前述权利要求中的任意一项的方法，其特征在于蒸发的液体是氧、氮或氩。
10.用于在至少约30巴的高压下生产气体的设备，这种设备包括一个带有一个低压工作塔(11)和一个中压工作塔(10)的空气双蒸馏塔(1)，一个用于压缩从设备的一个塔(11)中抽出的液体的泵(9)，用于压缩进入的空气的装置(14，30，31)，一个用于使待蒸馏的空气和压缩的液体进行热交换的焊接板式换热器(2)，以及用于从设备中至少抽出一种液体产品的管道(24，25；37A)，其特征在于压缩装置包括分别用来以中压、过渡压力和高压形成三股空气流的装置(4，6，7)，热交换器(2)包括从其热端到其冷端冷却中压空气的通道(13)、过渡压力下部分冷却空气的通道(14)和从其热端到其冷端冷却高压空气的通道(17)，以及该设备包括一个用来使至少一部分在过渡压力下的部分冷却空气膨胀至中压的透平机(8)和一个与双塔(1)相连的生产液态氩的塔(31)。
11.如权利要求10所述的设备，其特征在于该设备还包括一个用于通过蒸发从塔(11)中抽出的液体来使从中压塔(10)的贮槽中抽出的液体过冷的辅助热交换器(38)。
12.在高压下生产气体的方法，以这种方法，空气在带有一个双馏塔(1)的设备中蒸馏，该双馏塔(1)又包括一个低压工作的塔(11)和一个中压工作的塔(10)，其中部分空气在进入中压塔前在透平机(6)中膨胀至中压，所选择的空气压力应使空气的温度在透平机叶轮的入口处接近其自身的露点温度。
13.如权利要求12所述的方法，其中须在透平机中膨胀的空气在其利用双塔所产生的气体膨胀前，也可在增压和蒸发阶段之后被冷却。
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CN102192637A (zh) * 2010-03-19 2011-09-21 普莱克斯技术有限公司 空气分离方法和设备
CN102564064A (zh) * 2010-11-25 2012-07-11 林德股份公司 通过低温分离空气获得气态压力产物的方法
CN102538396A (zh) * 2010-12-13 2012-07-04 乔治洛德方法研究和开发液化空气有限公司 用于生产高压氮的方法和设备
CN102538396B (zh) * 2010-12-13 2016-01-20 乔治洛德方法研究和开发液化空气有限公司 用于生产高压氮的方法和设备
CN102721263A (zh) * 2012-07-12 2012-10-10 杭州杭氧股份有限公司 一种利用深冷技术分离空气的系统及方法

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EP0789208A1 (fr) 1997-08-13
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ZA971031B (en) 1997-08-25
JPH09310970A (ja) 1997-12-02
CN1097715C (zh) 2003-01-01
ES2193336T3 (es) 2003-11-01
US5735142A (en) 1998-04-07
DE69719578D1 (de) 2003-04-17
EP0789208B1 (fr) 2003-03-12
KR970062629A (ko) 1997-09-12
CA2197156A1 (en) 1997-08-13
FR2744795A1 (fr) 1997-08-14
DE69719578T2 (de) 2003-12-11

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