CN200979332Y - 含空气煤层气液化分离设备 - Google Patents

含空气煤层气液化分离设备 Download PDF

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CN200979332Y
CN200979332Y CNU2006201342971U CN200620134297U CN200979332Y CN 200979332 Y CN200979332 Y CN 200979332Y CN U2006201342971 U CNU2006201342971 U CN U2006201342971U CN 200620134297 U CN200620134297 U CN 200620134297U CN 200979332 Y CN200979332 Y CN 200979332Y
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air
separation equipment
heat exchanger
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杨克剑
张武
任小坤
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Technical Institute of Physics and Chemistry of CAS
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BEIJING KERUI SAISI GAS LIQUEFACTION TECHNOLOGY Co Ltd
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Abstract

本实用新型公开了一种含空气煤层气的液化分离设备，包括压缩净化设备、制冷设备和液化分离设备，所述液化分离设备包括第一分馏塔与换热器相连，第一分馏塔顶部具有冷凝器、底部具有蒸发器，第一分馏塔顶部出口连接有第二分馏塔，第二分馏塔顶部具有冷凝蒸发器。本实用新型含空气煤层气液化分离设备是专为含空气煤层气设计的分离液化过程，采用双级精馏设备，第一级分馏塔先分离甲烷和空气，得到纯度极高的液态煤层气，第二级分馏塔再分离空气中的氮气和其它组分，得到纯度极高的氮气；该套设备利用含空气煤层气的三组分特点而设计，分离效率高，设备简单，所得产品纯度高，适宜推广应用。

Description

含空气煤层气液化分离设备
技术领域
本实用新型涉及一种气体液化分离设备，特别涉及含空气煤层气的液化分离设备。
背景技术
煤层气也称非常规天然气或矿井瓦斯，其主要成分是甲烷。它不仅是一种宝贵的清洁能源，也是重要的化工原料。我国的煤层气资源极为丰富，但开发的比较少，几乎没有工业上的应用。据了解，我国每年排入大气的煤层气占全世界采煤排放的煤层气总量的三分之一，这不但造成了严重的大气污染，也是很大的资源浪费。
煤层气的特点是单井产量不很高，除就近使用外，铺设管道外输常常不合算。尤其是采煤过程中抽放的煤层气，因为压力低，甲烷含量低，而且其中混有空气，空气中的氧气是危险的助燃剂，这就给煤层气的加工和运输带来了困难，放空浪费的就更严重，这个问题一直没有得到很好的解决。如果把含空气煤层气中的煤层气(主要是甲烷)和空气分离出来并将提纯后的煤层气液化，这就极大地方便了运输和利用。
液化天然气技术从上世纪六十年代就开始商业化，至今已有三、四十年的历史。我国液化天然气产业正处于发展阶段，国内对各种液化天然气的循环已基本掌握。但不论是国外或者国内，液化天然气技术都是针对纯度较高、不含空气的天然气。对含空气的煤层气的分离和液化，还没有引起人们的重视，含空气煤层气放空排放的现象仍然十分严重。
常规的分离方法有吸收法、吸附法、薄膜渗透法和低温精馏法等。前面几种方法，分离的纯度很难达到要求，有的回收率低，有的还需要加热，含空气煤层气在高温下易爆炸，存在安全隐患，因此没有得到应用。
实用新型内容
本实用新型所要解决的技术问题是提供一种含空气煤层气的液化分离设备，采用低温双级精馏设备，双塔分别分离含空气煤层气中的煤层气和空气、氮气和含氧空气。使用该设备分离含空气煤层气，其液化煤层气的产品纯度可以达到99.9％以上，排放的空气中甲烷含量小于万分之一，整套设备简单、操作简便。
为解决上述技术问题，本实用新型所采取的技术方案是：
一种含空气煤层气液化分离设备，包括压缩净化设备、制冷设备和液化分离设备，所述液化分离设备包括有换热器，压缩净化设备的原料气输出管路与液化分离设备中的热介质通道连接，制冷设备的制冷气管路与液化分离设备的换热器冷介质通道连接，所述液化分离设备包括第一分馏塔与换热器相连，第一分馏塔顶部具有冷凝器、底部具有蒸发器，第一分馏塔顶部出口连接有第二分馏塔，第二分馏塔顶部具有冷凝蒸发器。
其中，所述第二分馏塔底部出口通过设有节流减压阀的管路依次连接第二分馏塔顶部的冷凝蒸发器的冷介质通道以及制冷设备的换热器冷介质通道；所述第二分馏塔顶部的气体出口连接换热器的冷介质通道；所述制冷设备为气体膨胀制冷设备或混合制冷剂制冷设备；所述第一份分馏塔的冷凝器与蒸发器的冷介质通道均与制冷设备相连。
本实用新型所能达到的有益效果是：本实用新型含空气煤层气液化分离设备是专为含空气煤层气设计的分离液化过程，采用双级精馏设备，第一级分馏塔先分离甲烷和空气，得到纯度极高的液态煤层气，第二级分馏塔再分离空气中的氮气和其它组分，得到纯度极高的氮气；该套设备利用含空气煤层气的三组分特点而设计，分离效率高，设备简单，所得产品纯度高，适宜推广应用。
附图说明
图1为本实用新型实施例1和实施例2压缩净化设备示意图；
图2为本实用新型实施例1制冷设备和液化分离设备示意图；
图3为本实用新型实施例2制冷设备和液化分离设备示意图。
具体实施方式
实施例1
参阅图1、图2，为本实用新型实施例1含空气煤层气液化分离设备示意图，包括三部分，压缩净化设备、制冷设备和液化分离设备。(图中虚线连接的两设备表示两者为同一设备)
参阅图1，为本实用新型实施例1压缩净化设备示意图。包括过滤器1、气液分离器2、压缩机3、冷却器4、气液分离器5、分子筛设备组，所述分子筛干燥设备组包括二台分子筛干燥机6、7，当第一台分子筛干燥机6工作时，第二台分子筛干燥机7加热再生然后冷却备用，每8小时切换一次。该分子筛干燥设备主要用来脱除水、二氧化碳。分子筛设备组后连接有过滤器9，还有加热器8。
压缩净化设备的工艺流程如下：
1、自排放管道来的含空气煤层气原料气首先经过滤器1除去灰尘；
2、除尘后的含空气煤层气进入气液分离器2气液分离后，气体进入压缩机3压缩；
3、压缩后经冷却器4冷却，再经过气液分离器5，除去游离水。
4、含空气煤层气进入分子筛干燥机6，脱出水和二氧化碳，流程中产生的氮气的一部分经加热器8加热至240-250℃，用于分子筛干燥机7的再生，直接进入已再生好的干燥机7，冷却分子筛，降低分子筛干燥机7的温度后备用；分子筛干燥机6和7切换使用。
5、经分子筛干燥设备脱除水、二氧化碳和氧气的含空气煤层气原料气再经过滤器9即可进入制冷、液化分离设备。
参阅图2，为本实用新型实施例1含空气煤层气制冷设备和液化分离设备示意图。液化分离设备包括依次连接的换热器10、11、12，制冷设备得到的冷量通过换热器10、11、12与换热器内的含空气煤层气热交换。换热器10、11、12后连接两级分馏塔14、15，第一分馏塔14具有冷凝器17和蒸发器16，第二分馏塔15具有冷凝蒸发器18，第一分馏塔顶部14与第二分馏塔15下部通过管路相连，第一分馏塔14的蒸发器16还具有液体管路将液体甲烷通过一换热器13过冷后，引入到储槽中。第二分馏塔15的顶部有管路与换热器13相连，第二分馏塔15的底部通过节流减压阀19与塔顶的冷凝蒸发器18相连。该液化分离设备在第一分馏塔中完成煤层气和空气的分离，在第二分馏塔中完成空气中的氮气和其它气体的分离。
上述液化分离设备的工作流程如下：
1、经压缩净化的含空气煤层气原料气，进入换热器10、11、12中交换热量，温度降低。
2、含空气煤层气自换热器中12出来后，进入第一分馏塔14，气体部分自下而上经过塔板，在第一分馏塔14顶部的冷凝器17(冷凝器17的冷量由制冷设备提供)内含空气煤层气被部分冷凝为液体，液体在塔中向下流动；
3、液体在第一分馏塔14底部的蒸发器16中被蒸发(蒸发器的热量由制冷系统的氮气提供)成为第一分馏塔的气体馏分，自下而上流过塔板，与向下走的液体进行热、质交换；这样越向上，气体中的甲烷含量越少，越向下，液体中的甲烷含量越多；
4、从第一分馏塔底部引出的是甲烷(甲烷纯度为99.99％)液体，温度为-143.8℃，通过一换热器13过冷后，成为过冷的液态甲烷输出，可进入储槽储存利用；第一分馏塔14塔顶气体是未被液化的空气，经一节流减压阀减压后进入第二分馏塔15的下部；
5、从含空气煤层气中分离出的未被液化的空气进入第二分馏塔15的下部，第二分馏塔是一个典型的带冷凝蒸发器18的空气分馏塔。空气自下而上流过每一块塔板，冷凝蒸发器18将一部分气体冷凝成为液体馏分向下流。液体馏分与向上流动的气体馏分接触进一步精馏，即在第二分馏塔15底部得到富氧的液体空气，顶部得到未被冷凝的纯净的氮气(含量可达99.36％)。
6、第二分馏塔15底部出来的富氧的液体空气经节流减压阀19减压后进入第二分馏塔塔顶的冷凝蒸发器18中被蒸发，使部分气体冷凝成液体馏分。氮气从塔15顶出来，先经过换热器13冷却液体甲烷，然后经一节流减压阀26节流(也可以经膨胀机膨胀)，压力降低，温度也进一步降低，然后它与制冷设备的氮气汇合进入换热器；
7、富氧的液体空气在冷凝蒸发器18中蒸发后，进入制冷设备作为冷介质回用后，放空。
上述液化分离过程中换热器10、11、12和冷凝器16所需要的冷量是由制冷设备提供的。所述制冷设备包括依次连接的压缩机20、冷却器24、透平增压机21、冷却器25，在冷却器25后面，管道分为两路，一路连接换热器10，另一路连接换热器22。换热器10管道连接蒸发器16的加热管道，然后再连接换热器11，再与换热器22的氮气管道合并，连接到透平膨胀机23的入口，透平膨胀机23的出口管道与阀门26出口管道合并，再连接到冷凝器17的冷气管道，然后再依次连接换热器12、11、10。换热器10热端的氮气排气管道分为两路，一路进压缩机入口，一路连接分子筛干燥器的再生管路。
制冷设备的工作流程如下：
1、制冷系统启动之前，系统内充满氮气作为制冷气。
2、启动制冷系统，制冷气先经压缩机20压缩、经冷却器24冷却，再经过透平增压机21增压、经冷却器25冷却，然后分为两路，一路进入第一换热器10预冷，一路进换热器22预冷；
3、制冷气从换热器10出来，再经蒸发器16，被蒸发器中的液体所冷却(同时也使液体蒸发)，温度下降，再进入换热器11，温度又下降，然后它与换热器22预冷的氮气汇合，进入透平膨胀机23膨胀制冷，此时，温度进一步下降，然后与阀门26出来的冷氮气汇合，先进入冷凝器17，为第一分馏塔14的塔顶提供冷源，然后进入换热器12的冷端，再依次进入换热器11、10；
4、制冷气进入换热器10复热后，多余的氮气连接到干燥器的再生管路，用于干燥器的加热再生和冷却，大部分氮气则再压缩、增压、制冷、膨胀制冷，如此循环。
由于流程中本身能够产生氮气，足够用来补充制冷系统的泄漏，因此启动以后，不需要再购买氮气。
实施例2
本实用新型实施例2的压缩净化设备与实施例1相同，图3为制冷设备和液化分离设备示意图。该套设备为简易的制冷和液化分离设备，制冷设备为混合制冷剂制冷设备，包括制冷机29和压缩机27，制冷设备的制冷气管路连接液化分离设备中的换热器28，液化分离设备还包括依次连接的两级分馏塔14、15，第一分馏塔14具有冷凝器17和蒸发器16，第二分馏塔15具有冷凝蒸发器18，第一分馏塔顶部14与第二分馏塔15下部通过管路相连，第一分馏塔14冷凝器17还具有液体管后路直接引入到储槽中。第二分馏塔15的底部有液体管路与塔顶的冷凝蒸发器18相连，第二分馏塔底部得到的液态空气经冷凝蒸发器18并回收热量后放空，顶部得到纯净的氮气可引入制冷设备中或放空。

Claims (5)

1、一种含空气煤层气液化分离设备，包括压缩净化设备、制冷设备和液化分离设备，所述液化分离设备包括有换热器，压缩净化设备的原料气输出管路与液化分离设备中的热介质通道连接，制冷设备的制冷气管路与液化分离设备的换热器冷介质通道连接，其特征在于，所述液化分离设备包括第一分馏塔与换热器相连，第一分馏塔顶部具有冷凝器、底部具有蒸发器，第一分馏塔顶部出口连接有第二分馏塔，第二分馏塔顶部具有冷凝蒸发器。
2、根据权利要求1所述的一种含空气煤层气液化分离设备，其特征在于，所述第二分馏塔底部出口通过设有节流减压阀的管路依次连接第二分馏塔顶部的冷凝蒸发器的冷介质通道以及制冷设备的冷介质通道。
3、根据权利要求1所述的一种含空气煤层气液化分离设备，其特征在于，所述第二分馏塔顶部的气体出口连接换热器的冷介质通道。
4、根据权利要求1所述的一种含空气煤层气液化分离设备，其特征在于，所述制冷设备为气体膨胀制冷设备或混合制冷剂制冷设备。
5、根据权利要求1所述的一种含空气煤层气液化分离设备，其特征在于，所述第一分馏塔的冷凝器与蒸发器均与制冷设备的冷介质通道相连。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101290184B (zh) * 2008-06-05 2010-10-13 北京国能时代能源科技发展有限公司 一种化工尾气的液化分离方法及设备
WO2010060735A3 (en) * 2008-11-03 2012-08-30 Shell Internationale Research Maatschappij B.V. Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101290184B (zh) * 2008-06-05 2010-10-13 北京国能时代能源科技发展有限公司 一种化工尾气的液化分离方法及设备
WO2010060735A3 (en) * 2008-11-03 2012-08-30 Shell Internationale Research Maatschappij B.V. Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor

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