CN1102701A - 在加压下生产气态氧和/或气态氮的方法和装置 - Google Patents

在加压下生产气态氧和/或气态氮的方法和装置 Download PDF

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CN1102701A
CN1102701A CN94115629A CN94115629A CN1102701A CN 1102701 A CN1102701 A CN 1102701A CN 94115629 A CN94115629 A CN 94115629A CN 94115629 A CN94115629 A CN 94115629A CN 1102701 A CN1102701 A CN 1102701A
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A·吉拉德
N·里斯
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

在加压下生产气态氧和/或气态氮的方法中，空 气在双分馏塔(9)中分馏，泵送(在13中)至少一种从 低压塔(11)底部排出的液态产品，通过与加压到高压 的空气热交换的压缩的液态产品被汽化(在8中)，全 部待分馏的空气被加压缩到高压，过量的空气在串联 的两台透平机(5、6)中膨胀到中压塔(10)的压力，该 空气在这两台透平机间部分地再加热(在22中)。

Description

本发明涉及在加压下生产气态氧和/或气态氮的方法，在该方法中：
-空气在双分馏塔中分馏，该双分馏塔包括一台在所谓的低压下操作的低压塔和一台在所谓的中压下操作的中压塔;
-全部待分馏的空气被压缩到至少明显高于中压的高压;
-该压缩空气被冷却到中温，其中的一部分在其被送入中压塔之前在透平机中膨胀;
-未膨胀的空气被液化，在膨胀后被送入双分馏塔;和
-至少一种液态产品在生产压力下从双分馏塔排出，该液态产品通过与液化温度低于液态产品气化温度的空气进行热交换而被气化。
本说明书中所述及的压力均为绝对压力。此外，应从广义上理解措词“液化”，也就是说包括超临界压力下的准液化。
上述这种方法在FR-A-2  674  011中作了介绍。在该方法中，在加压生产气态产品的同时，必然伴随产生各种工业应用中所不希望有的液态产品。
本发明的目的在于，根据给定的加压生产气态氧和/或气态氮的能力，降低液态产品的产率，而不增加每种产品的比能。
为达到此目的，本发明提供了一种上述类型的方法，其特征在于仅将一部分空气膨胀到中压，膨胀作功后的空气再部分加热，然后在第二台透平机中膨胀到中压，并送入中压塔。
在本发明的实施方案中：
-所述中温显著地比所述液态产品的气化温度约低10℃;
-所述第二台透平机的进口温度约为空气液化拐点的温度。
本发明为实现其目的，还具有适合于实施这种方法的装置。该装置包括：一组双分馏塔，该塔包括一台在所谓的低压下操作的低压塔和一台在所谓的中压下操作的中压塔;压缩设备，可将全部待分馏的空气压缩到至少明显高于中压的高压，这些设备包括一台主空气压缩机;用于从双分馏塔排放和泵送至少一种在分馏过程中产生的液态产品的设备;一套热交换系统，用以使空气和所述液态产品进行热交换;一台用于使这部分空气膨胀的膨胀透平机，该透平机的进口连接到热交换系统的中部，其特征在于，该热交换系统包括进口连接到所述透平机出口的部分再加热管道，其特征还在于该装置包括第二台膨胀透平机，其进口连接到上述再加热管道的出口上，而其出口则连接到中压塔上。
根据本发明的其它特征：
-该两台透平机用键固定在同一条转轴上;
-该两台透平机的转轴固定到用于使来自主压缩机的空气增压的鼓风机的轮轴上。
现根据附图对本发明实施方案作详细说明，这张简单的示意图示出了根据本发明的加压生产气态氧的装置。
图中所示的装置适合于在约10-100巴的高压下生产气态氧、液态氧和液态氮。
该装置主要包括：一台主空气压缩机1;一台预冷却器2;一套采取吸附法进行净化的装置3;一套鼓风机-透平机机组，其中包括一台鼓风机4和两台转子固定在同一转轴上的透平机5、6;一台鼓风机用的空气或水冷制冷器7;一套热交换系统8;一台双分馏塔9，它包括一台中压塔10和一台低压塔11，其间由气化器-冷凝器12连接，该气化器-冷凝器用来使塔10顶部的氮气和塔11底部的液态氧进行热交换;一台液氧泵13;一台常压液态氧贮槽14;一台常压液态氮贮槽15;一台分相器16;以及一台过冷器17。
在操作中，塔11处于稍高于常压的压力下，而塔10则处于相当于约5-6巴的压力下。
全部待分馏的空气在1中被压缩，在2中预冷却到+5至+20℃，在3中净化除去其中的水分和二氧化碳并进一步在4中被压缩到高压。在7中预冷却后，在热交换系统的管道18中部分冷却到中温T1，一部分高压空气继续在热交换系统的管道19中冷却而被液化，然后被分成两部分。每一部分分别在膨胀阀20、21中膨胀，然后分别送入塔10、11。
在温度T1下，其余高压空气从热交换系统排出，在5中膨胀作功后降到中压，然后，再送入热交换系统，在该热交换的管道22中部分地再加热到等于或不等于T1的中温T2，然后，再从该热交换系统排出，在6中膨胀作功降到中压后送入塔10的底部。
T1可以特别地选择比氧的气化温度约低10℃，而T2则接近高压空气的液化拐点，该拐点低于氧的气化温度且低于T1。
按照已知的方法，从塔10底部排出的“富液”（富氧空气）和在该塔顶部排出的“贫液”（稍纯的氮气）在17中过冷却和分别在膨胀阀22和23中膨胀后，分别被送入塔11的中部和顶部。
液态氧从塔11的底部排放。一部分经管道24直接进入贮槽15，而其余部分用泵13加压到所需的高生产压力，在热交换系统的通管道25中气化并再加热到室温之后，再通过管道26排放。
此外，从塔10顶部排出的处于中压的液态氮，在17中过冷却，在膨胀阀27中膨胀到常压，然后送入分相器16。分离出的液相被送到贮槽15，而气相则与塔11顶部的不纯氮气混合，然后将该混合物在17、继而在热交换系统的管道28中再加热后，作为残余的废氮气WN2通过管道29从该装置中排放。
在40巴压力下，以每天生产248吨纯度为99.5%的氧气为基准进行计算，结果表明，与上述FR-A-2  674  011中单级透平机方案的30巴对比，空气的高压可降低到25.5巴。在相同的条件下，液态产品与分离氧的能力之比可从30%降到22%，而每种产品的比能仍可保持不变。
本发明还可以应用于在高压下生产气态氮，即通过泵（未示出）加压到所需的高压，然后在热交换系统中气化，和/或通过利用不同高压的空气，在不同的压力下生产氧和/或氮。

Claims (6)

1、一种在加压下生产气态氧和/或气态氮的方法，在该方法中：
-空气在双分馏塔(9)中分馏，该双分馏塔包括一台在所谓的低压下操作的低压塔(11)和一台在所谓的中压下操作的中压塔(10)；
-全部待分馏的空气被压缩(在1、4中)到至少明显高于中压的高压；
-该压缩空气被冷却到中温(T1)，其中的一部分在其被送入中压塔(10)之前在透平机(5)中膨胀到中压；
-未膨胀的空气被液化，膨胀(在20、21中)后被送入双分馏塔；和
-至少一种从双分馏塔排出的液态产品加压(在13中)到生产压力，该液态产品通过与液化温度低于液态产品气化温度的空气进行热交换(在8中)而被气化，其特征在于一部分所述空气仅膨胀到中压，膨胀作功后的空气再部分加热(在22中)，然后在第二台透平机(6)中膨胀到中压，并送入中压塔(10)。
2、根据权利要求1的方法，其特征在于所述中温（T1）显著地比所述液态产品的气化温度约低10℃。
3、根据权利要求1或2的方法，其特征在于所述第二台透平机（6）的进口温度（T2）接近空气液化拐点的温度。
4、一套在加压下生产气态氧和/或气态氮的装置，该装置包括：一组双分馏塔（9），该双分馏塔包括一台在所谓的低压下操作的低压塔（11）和一台在所谓的中压下操作的中压塔（10），这些设备包括主空气压缩机（1）;压缩设备（1、4），可将全部待分馏的空气压缩到至少明显高于中压的高压;用于从双分馏塔排放和泵送至少一种由分馏产生的液态产品的设备（13）;一套热交换系统（8），用以使空气和所述液态产品进行热交换;和用于使这部分空气膨胀的透平机（9），该透平机的进口连接到热交换系统的中部，其特征在于该热交换系统（8）包括其进口连接到所述透平机（5）的出口上的部分再加热的管道（22），其特征还在于该装置包括第二台膨胀透平机（6），该透平机的进口连接到上述再加热管道的出口，而其出口则连接到中压塔（10）上。
5、根据权利要求4的装置，其特征在于该两台透平机（5、6）用键固定在同一个转轴上。
6、根据权利要求5的装置，其特征在于该两台透平机（5、6）的转轴固定到用于使来自主压缩机（1）的空气增压的鼓风机（4）的轮轴上。
CN94115629A 1993-09-01 1994-08-31 在加压下生产气态氧和/或气态氮的方法和装置 Pending CN1102701A (zh)

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CN106595221A (zh) * 2015-10-20 2017-04-26 乔治洛德方法研究和开发液化空气有限公司 制氧系统和制氧方法

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FR2795495B1 (fr) * 1999-06-23 2001-09-14 Air Liquide Procede et installation de separation d'un melange gazeux par distillation cryogenique
JP4594360B2 (ja) * 2007-08-27 2010-12-08 神鋼エア・ウォーター・クライオプラント株式会社 深冷空気液化分離装置およびその運転方法
FR2928446A1 (fr) * 2008-03-10 2009-09-11 Air Liquide Procede de modification d'un appareil de separation d'air par distillation cryogenique
CN104406365B (zh) * 2014-11-27 2017-04-05 苏州制氧机股份有限公司 一种双膨胀机中压液体设备

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CN102741636A (zh) * 2009-08-11 2012-10-17 林德股份公司 用于通过低温分离空气产生气态氧加压产品的方法和设备
CN106595221A (zh) * 2015-10-20 2017-04-26 乔治洛德方法研究和开发液化空气有限公司 制氧系统和制氧方法

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FR2709537A1 (fr) 1995-03-10
US5477689A (en) 1995-12-26
EP0641983B1 (fr) 1997-04-16
DE69402643T2 (de) 1997-10-02
DE69402643D1 (de) 1997-05-22
JPH07151458A (ja) 1995-06-16
CA2131120A1 (fr) 1995-03-02
FR2709537B1 (fr) 1995-10-13
ES2102790T3 (es) 1997-08-01
EP0641983A1 (fr) 1995-03-08

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