CN101929788B - 含氧煤层气制取液化天然气的装置 - Google Patents
含氧煤层气制取液化天然气的装置 Download PDFInfo
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Abstract
本发明公开了一种含氧煤层气制取液化天然气的装置,包括压缩净化工序和液化分离工序,液化分离工序包括主流程工艺和制冷工艺,制冷工艺中采用混合制冷剂结合节流制冷以及特殊的制冷剂流程;本发明制冷工艺采用混合制冷并结合节流制冷,改变现有的制冷工艺,充分并合理的利用工艺过程中的冷量回收过程,提高制冷效率,从而相对提高装置的处理能力,对于单井产量不高的煤层气而言,可节约生产成本,只利用一套压缩设备,节约动力能源。
Description
技术领域
本发明涉及一种利用液化原理进行分离的方法,尤其涉及一种含氧煤层气液化回收的装置。
背景技术
含氧煤层气是煤矿在开采过程中为防止瓦斯爆炸和突出,保证煤矿安全生产而抽排出的初级副产品;其主要成分为甲烷,从其成分含量上可以看出,煤层气是较为重要的能源和化工原料。但是由于其成分较为复杂,特别是在煤层气中含有氧,是非常危险的助燃助爆剂,制约了含氧煤层气的综合利用;实践中,为了节约成本,煤层气普遍在采煤过程中排入大气,造成资源的极度浪费和对环境造成污染。
随着科学技术的发展,出现了多种含氧煤层气的液化技术。其中,ZL200610103425.0的专利公开了低温精馏法应用于含氧煤层气的分离和液化,具有分离纯度高,装置结构简单的优点。
但是,该制冷工艺采用混合制冷或者膨胀制冷等常规的制冷方式,结构复杂,透平膨胀集等辅助机械,制冷效率较低,降低了分离和液化装置的处理能力。
因此,需要对现有的含氧煤层气的液化工艺进行改进,改变现有的制冷工艺,充分并合理的利用工艺过程中的冷量回收过程,提高制冷效率,从而相对提高装置的处理能力,对于单井产量不高的煤层气而言,可节约生产成本。
发明内容
有鉴于此,本发明提供了一种含氧煤层气制取液化天然气的装置,改变现有的制冷工艺,充分并合理的利用工艺过程中的冷量回收过程,提高制冷效率,从而相对提高装置的处理能力,对于单井产量不高的煤层气而言,可节约生产成本。
本发明的一种含氧煤层气制取液化天然气的装置,包括压缩净化系统和液化分离系统;
压缩净化系统包括依次串接的水封罐、原料气压缩机、原料气除酸吸收塔和变压吸附系统;
液化分离系统包括主流程系统和制冷系统;
所述主流程系统包括依次串接的一级换热器、二级换热器、三级换热器和精馏塔,变压吸附系统的净化后含氧煤层气出口连通于一级换热器,位于精馏塔塔顶设置连通于精馏塔顶氮氧气出口的塔顶冷凝器,所述精馏塔塔内位于塔底设置再沸器,精馏塔塔底设置冷凝液出口;
制冷系统包括混合制冷剂平衡罐、制冷剂压缩机、制冷剂冷却器、制冷剂一次气液分离器和制冷剂二次气液分离器,制冷剂压缩机入口连通于制冷剂平衡罐,制冷机压缩机出口通过制冷剂冷却器连通于制冷剂一次气液分离器,制冷剂一次气液分离器气体出口通过一级换热器连通于二次气液分离器,二次气液分离器气体出口依次经过二级换热器、再沸器、三级换热器和一节流阀Ⅲ连通于塔顶冷凝器,塔顶冷凝器制冷剂出口依次经过三级换热器、二级换热器和一级换热器连通于混合制冷剂平衡罐使制冷剂回流循环使用;
混合制冷剂平衡罐内混合制冷剂按体积百分比包括:氮 35%,甲烷 30.65%,乙烯 16.81%,丙烷 3.8%,丁烷 8.17% 戊烷 5.57%;
一次气液分离器的液体出口依次经过一级换热器和一节流阀Ⅰ位于一级换热器和二级换热器之间连通于回流制冷剂;二次气液分离器的液体出口依次经过二级换热器和一节流阀Ⅱ位于二级换热器和三级换热器之间连通于回流制冷剂;
所述一级冷却器、二级冷却器、三级冷却器、再沸器和塔顶冷凝器均为按照介质种类设置流道的间壁式结构。
进一步,精馏塔塔顶氮氧气出口经过塔顶冷凝器连通于塔顶气液分离器,塔顶气液分离器氮氧气出口依次经过一成品冷却器、三级换热器、二级换热器和一级换热器连通于变压吸附系统;塔顶气液分离器液体出口连通于精馏塔;所述精馏塔塔底的冷凝液出口连通于成品冷却器;所述成品冷却器为间壁式结构。
进一步,原料气除酸吸收塔内用于吸收酸性气体的吸收液为一乙醇胺、二乙醇胺或甲基二乙醇胺水溶液;
进一步,变压吸附系统包括并联的三个吸附塔,吸附塔的吸附剂包括芳香烃吸附剂和硫浸煤基活性炭;
进一步,所述水封罐与原料气压缩机之间还设有气液分离器;原料气压缩机出口与原料气除酸吸收塔之间还设置原料气冷却器;原料气除酸吸收塔出口与变压吸附系统之间还顺序设置有塔后冷却器和塔后气液分离器;
进一步,所述原料气压缩机为两级压缩,制冷机压缩机为三级压缩;
进一步,所述变压吸附系统净化含氧煤层气出口通过一用于过滤微量吸附剂粉沫的分离器连通于一级换热器;
进一步,在主流程系统中,三级换热器和精馏塔之间设置节流阀Ⅳ。
本发明的有益效果在于:本发明结构的含氧煤层气制取液化天然气的装置,制冷工艺采用混合制冷并结合节流制冷,改变现有的制冷工艺,充分并合理的利用工艺过程中的冷量回收过程,提高制冷效率,从而相对提高装置的处理能力,对于单井产量不高的煤层气而言,可节约生产成本,只利用一套压缩设备,节约动力能源。
附图说明
下面结合附图和具体实施方式对本发明作进一步详细的说明。
图1为本发明压缩净化系统结构示意图;
图2为本发明液化分离系统结构示意图。
具体实施方式
图1为本发明压缩净化系统结构示意图,图2为本发明液化分离系统结构示意图,如图所示:本实施例的含氧煤层气制取液化天然气的装置,包括压缩净化系统和液化分离系统;
压缩净化系统包括依次串接的水封罐1、原料气压缩机3、原料气除酸吸收塔5和变压吸附系统;如图所示,变压吸附系统包括并联的吸附塔8、吸附塔9和吸附塔10,当然,可以是其它数量的吸附塔进行连接使用;
液化分离系统包括主流程系统和制冷系统;
所述主流程系统包括依次串接的一级换热器12、二级换热器13、三级换热器4和精馏塔16,变压吸附系统的净化后含氧煤层气出口连通于一级换热器12,位于精馏塔16塔顶设置连通于精馏塔顶氮氧气出口的塔顶冷凝器20,所述精馏塔16塔内位于塔底设置再沸器17,精馏塔16塔底设置冷凝液出口;
制冷系统包括混合制冷剂平衡罐22、制冷剂压缩机23、制冷剂冷却器24、制冷剂一次气液分离器25和制冷剂二次气液分离器27,制冷剂压缩机23入口连通于制冷剂平衡罐22,制冷机压缩机23出口通过制冷剂冷却器24连通于制冷剂一次气液分离器25,制冷剂一次气液分离器25气体出口通过一级换热器12连通于二次气液分离器27,二次气液分离器27气体出口依次经过二级换热器13、再沸器17、三级换热器14和一节流阀Ⅲ29连通于塔顶冷凝器20,塔顶冷凝器20制冷剂出口依次经过三级换热器14、二级换热器13和一级换热器12连通于混合制冷剂平衡罐22使制冷剂回流循环使用;
混合制冷剂平衡罐22内混合制冷剂按质量百分比包括:氮 35%,甲烷 30.65%,乙烯 16.81%,丙烷 3.8%,丁烷 8.17% 戊烷 5.57%;本配比能合理分配制冷剂中各个成分在各个环节的气液成分,合理控制流程中的温度指标;
一次气液分离器25的液体出口依次经过一级换热器12和一节流阀Ⅰ26位于一级换热器12和二级换热器13之间连通于回流制冷剂;二次气液分离器27的液体出口依次经过二级换热器13和一节流阀Ⅱ28位于二级换热器13和三级换热器14之间连通于回流制冷剂;
所述一级冷却器12、二级冷却器13、三级冷却器14、再沸器17和塔顶冷凝器20均为按照介质种类设置流道的间壁式结构;各个通过介质之间完全独立且可互相之间交换热量。
本实施例中,精馏塔16塔顶氮氧 气出口经过塔顶冷凝器20连通于塔顶气液分离器21,塔顶气液分离器21氮氧气出口依次经过一成品冷却器18、三级换热器14、二级换热器13和一级换热器12连通于变压吸附系统;塔顶气液分离器21液体出口连通于精馏塔16,用于冷凝液回流至精馏塔;所述精馏塔16塔底的冷凝液出口连通于成品冷却器18;所述成品冷却器18为间壁式结构;通过成品冷却器18过冷产品并通过三级换热器14、二级换热器13和一级换热器12回收冷量,充分利用低温氮氧气的冷量,进一步提高冷却效率,并使氮氧气最终温度升高,并适用于下级流程。
本实施例中,原料气除酸吸收塔23内用于吸收酸性气体的吸收液为一乙醇胺、二乙醇胺或甲基二乙醇胺水溶液,本实施例为二乙醇胺水溶液。
本实施例中,变压吸附系统包括并联的三个吸附塔,吸附塔的吸附剂包括芳香烃吸附剂和硫浸煤基活性炭;利于除去杂质,防止影响最终产品质量;同时提高吸附工序的效率。
本实施例中,所述水封罐1与原料气压缩机3之间还设有气液分离器2,防止压缩机3出现液击现象,保证其安全运行;原料气压缩机3出口与原料气除酸吸收塔5之间还设置原料气冷却器,较低的温度利于原料气除酸吸收塔5正常吸收;原料气除酸吸收塔5出口与变压吸附系统之间还顺序设置有塔后冷却器6和塔后气液分离器7,冷却并气液分离后可进来那个减少带入吸附塔的杂质,为吸附净化提供良好的吸附条件。
本实施例中,所述原料气压缩机3为两级压缩,制冷机压缩机23为三级压缩,级间均设置冷却及气液分离器,降低压缩气体的单级压缩比,以及单级出口的温度,从而降低能耗;
本实施例中,所述变压吸附系统净化含氧煤层气出口通过一用于过滤微量吸附剂粉沫的分离器11连通于一级换热器12,保证净化含氧煤层气的洁净,避免影响换热器的换热效率。
本实施例中,在主流程系统中,三级换热器14和精馏塔16之间设置节流阀Ⅳ15,节流降压后进一步降低温度,利于冷凝和分离。
本发明在生产时,包括:
A.压缩净化工序:将来自煤矿的低浓度含氧煤层原料气经水封罐1混合式水冷、原料气压缩机3压缩和原料气除酸吸收塔5和变压吸附系统净化去除杂质得到净化含氧煤层气;吸收塔内的吸收液为醇胺水溶液,用于脱出酸性气体;脱出酸性气体后的原料气通过吸附塔内的吸附剂脱除原料其中的芳香烃;同时,吸附塔中加入硫浸煤基活性炭用于脱除原料气中的汞,得到主要成分为CH4 、N2 和O2的净化含氧煤层气;
B.液化分离工序:
液化分离工序包括:
B1.主流程工艺:将净化含氧煤层气依次通过一级换热器、二级换热器和三级换热器冷却,,形成冷凝液和气体的混合物,出换热器净化含氧煤层气经过节流阀Ⅲ29节流后进入精馏塔;精馏塔塔底得到液化天然气,剩余冷凝液由塔底流出经成品冷却器冷却后即为成品液化天然气;塔顶得到N2 和O2混合气并含有少量CH4进入塔顶冷凝器20;
精馏塔16顶流出的N2 和O2进入塔顶冷凝器20析出携带出的少量CH4组分,有塔顶气液分离器21进行气液分离后,液态为CH4由精馏塔16顶回流至至塔内;分离掉液态CH4后N2 和O2通过成品冷却器18冷却精馏塔底出来的液化天然气后依次通过三级换热器14、二级换热器13和一级换热器12回收冷量后温度为进入变压吸附系统,作为吸附塔中吸附剂再生时的冷吹气体。
B2.制冷工艺:
B21. 制冷剂平衡罐22的混合制冷剂经制冷剂压缩机23压缩、制冷剂冷却器24冷却;一次气液分离器25一次气液分离后,气态进入一级换热器冷却,进入二次气液分离器27二次气液分离后,气态进入二级换热器冷却后进入精馏塔底的再沸器17,加热塔底冷凝液后自身被冷却后,进入三级换热器14冷却,先进入塔底再沸器冷却后再进入三级换热器冷却,可减小三级换热器的负荷,保证原料气的冷却效果,同时加热了塔底冷凝液,提高精馏和制冷效率,相对提高装置的处理能力;三级换热器14冷却后经节流降压后降温进入塔顶冷凝器6冷却塔顶出口的N2 和O2及少量CH4组分,依次经过三级换热器6、二级换热器13和一级换热器12逐渐换热并回流至压缩入口循环使用;
B22.一次气液分离后的液体进入一级换热器12冷却经节流阀Ⅰ26节流后由一级换热器和二级换热器之间进入回流制冷剂回流;二次气液分离后的液体进入二级换热器13冷却,经节流阀Ⅱ28节流后降压后由二级换热器13和三级换热器14之间进入回流制冷剂回流;通过节流降低压力从而达到蒸发降温的目的,并不需要额外的设备和动力,节约能源,减小设备和占地投入。
最后说明的是,以上实施例仅用以说明本发明的技术方案而非限制,尽管参照较佳实施例对本发明进行了详细说明,本领域的普通技术人员应当理解,可以对本发明的技术方案进行修改或者等同替换,而不脱离本技术方案的宗旨和范围,其均应涵盖在本发明的权利要求范围当中。
Claims (8)
1.一种含氧煤层气制取液化天然气的装置,其特征在于:包括压缩净化系统和液化分离系统;
压缩净化系统包括依次串接的水封罐、原料气压缩机、原料气除酸吸收塔和变压吸附系统;
液化分离系统包括主流程系统和制冷系统;
所述主流程系统包括依次串接的一级换热器、二级换热器、三级换热器和精馏塔,变压吸附系统的净化后含氧煤层气出口连通于一级换热器,位于精馏塔塔顶设置连通于精馏塔顶氮氧气出口的塔顶冷凝器,所述精馏塔塔内位于塔底设置再沸器,精馏塔塔底设置冷凝液出口;
制冷系统包括混合制冷剂平衡罐、制冷剂压缩机、制冷剂冷却器、制冷剂一次气液分离器和制冷剂二次气液分离器,制冷剂压缩机入口连通于制冷剂平衡罐,制冷机压缩机出口通过制冷剂冷却器连通于制冷剂一次气液分离器,制冷剂一次气液分离器气体出口通过一级换热器连通于二次气液分离器,二次气液分离器气体出口依次经过二级换热器、再沸器、三级换热器和一节流阀Ⅲ连通于塔顶冷凝器,塔顶冷凝器制冷剂出口依次经过三级换热器、二级换热器和一级换热器连通于混合制冷剂平衡罐使制冷剂回流循环使用;
混合制冷剂平衡罐内混合制冷剂按体积百分比包括:氮 35%,甲烷 30.65%,乙烯 16.81%,丙烷 3.8%,丁烷 8.17%,戊烷 5.57%;
一次气液分离器的液体出口依次经过一级换热器和一节流阀Ⅰ位于一级换热器和二级换热器之间连通于回流制冷剂;二次气液分离器的液体出口依次经过二级换热器和一节流阀Ⅱ位于二级换热器和三级换热器之间连通于回流制冷剂;
所述一级换热器、二级换热器、三级换热器、再沸器和塔顶冷凝器均为按照介质种类设置流道的间壁式结构。
2.根据权利要求1所述的含氧煤层气制取液化天然气的装置,其特征在于:精馏塔塔顶氮氧气出口经过塔顶冷凝器连通于塔顶气液分离器,塔顶气液分离器氮氧气出口依次经过一成品冷却器、三级换热器、二级换热器和一级换热器连通于变压吸附系统;塔顶气液分离器液体出口连通于精馏塔;所述精馏塔塔底的冷凝液出口连通于成品冷却器;所述成品冷却器为间壁式结构。
3.根据权利要求2所述的含氧煤层气制取液化天然气的装置,其特征在于:原料气除酸吸收塔内用于吸收酸性气体的吸收液为一乙醇胺、二乙醇胺或甲基二乙醇胺水溶液。
4.根据权利要求3所述的含氧煤层气制取液化天然气的装置,其特征在于:变压吸附系统包括并联的三个吸附塔,吸附塔的吸附剂包括芳香烃吸附剂和硫浸煤基活性炭。
5.根据权利要求4所述的含氧煤层气制取液化天然气的装置,其特征在于:所述水封罐与原料气压缩机之间还设有气液分离器;原料气压缩机出口与原料气除酸吸收塔之间还设置原料气冷却器;原料气除酸吸收塔出口与变压吸附系统之间还顺序设置有塔后冷却器和塔后气液分离器。
6.根据权利要求5所述的含氧煤层气制取液化天然气的装置,其特征在于:所述原料气压缩机为两级压缩,制冷机压缩机为三级压缩。
7.根据权利要求6所述的含氧煤层气制取液化天然气的装置,其特征在于:所述变压吸附系统净化含氧煤层气出口通过一用于过滤微量吸附剂粉末的分离器连通于一级换热器。
8.根据权利要求7所述的含氧煤层气制取液化天然气的装置,其特征在于:在主流程系统中,三级换热器和精馏塔之间设置节流阀Ⅳ。
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CN103307854A (zh) * | 2013-06-08 | 2013-09-18 | 中煤科工集团重庆研究院 | 低浓度煤层气液化浓缩用防爆型精馏塔 |
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