CN103484184A - 含氧煤层气的脱氧、脱氮系统 - Google Patents

含氧煤层气的脱氧、脱氮系统 Download PDF

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CN103484184A
CN103484184A CN201310400700.5A CN201310400700A CN103484184A CN 103484184 A CN103484184 A CN 103484184A CN 201310400700 A CN201310400700 A CN 201310400700A CN 103484184 A CN103484184 A CN 103484184A
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azeotrope
ice chest
gas
deoxidation
nitrogen
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CN103484184B (zh
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单彤文
陈杰
曾伟平
尹全森
花亦怀
冯颉
李秋英
常心洁
程昊
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China National Offshore Oil Corp CNOOC
CNOOC Gas and Power Group Co Ltd
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CNOOC Gas and Power Group Co Ltd
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Abstract

本发明公开了一种含氧煤层气的脱氧、脱氮系统。所述系统包括冷箱、精馏塔、煤层气脱氧、脱氮机构、混合冷剂循环机构和氮气冷剂循环机构；混合冷剂循环机构为冷箱提供冷量；氮气冷剂循环机构为冷箱和精馏塔提供冷量；煤层气脱氧、脱氮机构包括原料气管线、设置于精馏塔塔顶的再冷凝器和设置于精馏塔塔底的再沸器；原料气管线与所述冷箱相连通，然后从冷箱中引出后与再沸器相连通；原料气管线从再沸器引出后再进入至冷箱中，然后从冷箱中引出后与精馏塔相连通；再沸器的气相出口通过管路与冷箱相连通，管路经冷箱冷却后与LNG储罐相连通。本发明可实现原料气甲烷含量在30～90%混空煤层气的液化，减少碳排放，最大限度回收天然气资源。

Description

含氧煤层气的脱氧、脱氮系统
技术领域
本发明涉及一种含氧煤层气的脱氧、脱氮系统，属于天然气液化技术领域。
背景技术
在煤矿开采过程中抽采的煤层气，甲烷含量比较低，通常为30%～70%（体积分数），其他成分主要包括二氧化碳和空气。2010年我国井下抽采煤层气76亿方，利用量约24.3亿方，利用量不足32%。我国煤层气资源丰富，但开发的比较少，几乎没有工业应用。由于煤层气涌入煤矿巷道或爆炸会引起灾难，因此，煤炭工业界一直将煤层气视为灾害气体。目前这种混有空气的含氧煤层气的抽放处理仅仅是基于煤矿的安全生产要求而进行的，绝大部分排放到大气中，但是由于数量巨大，不仅浪费资源，而且还会引起温室效应。除就近使用外，通过管道外输十分不经济，如果将含氧煤层气中的煤层气与空气（主要为氧气、氮气）分离液化，就能将含氧煤层气利用起来，可以极为方便的运输和利用。
目前已有几种关于含氧煤层气的分离工艺及设备的发明专利申请，例如200610080889.4号中国申请专利，该专利申请公开的技术方案采用低温双级精馏实现甲烷与空气的分离，但是采用双级精馏工艺流程复杂，设备较多，精馏塔压力损失较大，由于系统采用低压流程，所以工艺能耗较高。200610103425.0号中国专利申请采用低温精馏法应用于含氧煤层气的分离和液化，但是该工艺采用混合制冷或者膨胀制冷等常规的制冷方式，透平膨胀机等辅助机械制冷效率低，降低了分离和液化的处理能力。而20101028282232.2号中国专利申请采用混合冷剂结合节流制冷工艺，能一定程度上提高这冷效率，但是由于精馏塔顶再冷凝器所需温度极低，采用单一混合冷剂流程难以保证甲烷的回收率，从而造成甲烷的浪费，且工艺能耗较高。200910012669.1号中国专利申请采用催化脱氧，先让含氧煤层气中的甲烷与氧气反应，除去氧气。此工艺流程较为复杂，且需消耗大量的甲烷与氧气反应，而含有的N2还需要进一步处理。
发明内容
本发明的目的是提供一种含氧煤层气的脱氧、脱氮系统，使用本发明的系统进行脱氮、脱氧时，改变了现有的制冷工艺，其采用混合冷剂+N2节流制冷，充分利用工艺流程中的冷量回收，同时保证了甲烷回收率，具备换热效率高、能耗低、煤层气脱氧、脱氮精度高、甲烷回收率高、安全性高等特点。
为实现上述技术问题，本发明采用的技术方案如下：
本发明所提供的一种含氧煤层气的脱氧、脱氮系统，它包括冷箱、精馏塔、煤层气脱氧、脱氮机构、混合冷剂循环机构和氮气冷剂循环机构；
所述混合冷剂循环机构为所述冷箱提供冷量；
所述氮气冷剂循环机构为所述冷箱和所述精馏塔提供冷量；
所述煤层气脱氧、脱氮机构包括原料气管线、设置于所述精馏塔塔顶的再冷凝器和设置于所述精馏塔塔底的再沸器；所述原料气管线与所述冷箱相连通，然后从所述冷箱中引出后与所述再沸器相连通；所述原料气管线从所述再沸器引出后再进入至所述冷箱中，然后从所述冷箱中引出后与所述精馏塔相连通；所述再沸器的气相出口通过管路与所述冷箱相连通，所述管路经所述冷箱冷却后与LNG储罐相连通。
上述的脱氧、脱氮系统中，所述混合冷剂循环机构可为二级压缩单元。
上述的脱氧、脱氮系统中，所述二级压缩单元包括一级混合冷剂压缩机、二级混合冷剂压缩机、混合冷剂冷却器Ⅰ、混合冷剂冷却器Ⅱ、混合冷剂气液分离器Ⅰ和混合冷剂气液分离器Ⅱ；
所述一级混合冷剂压缩机的出口与所述混合冷剂冷却器Ⅰ相连通，所述混合冷剂冷却器Ⅰ的出口与所述混合冷剂气液分离器Ⅰ相连通；所述混合冷剂气液分离器Ⅰ的气相出口与所述二级混合冷剂压缩机的入口相连通，所述二级混合冷剂压缩机的出口与所述混合冷剂冷却器Ⅱ相连通，所述混合冷剂冷却器Ⅱ的出口和所述混合冷剂气液分离器Ⅰ的液相出口均与所述混合冷剂气液分离器Ⅱ相连通；所述混合冷剂气液分离器Ⅱ的气相出口和液相出口均与所述冷箱相连通，并进行节流，然后从所述冷箱中引出后与所述一级混合冷剂压缩机相连通。
上述的脱氧、脱氮系统中，所述氮气冷剂循环机构可为三级压缩单元。
上述的脱氧、脱氮系统中，所述三级压缩单元包括依次连通的一级氮气压缩机、氮气冷却器Ⅰ、二级氮气压缩机、氮气冷却器Ⅱ、三级氮气压缩机和氮气冷却器Ⅲ；
所述氮气冷却器Ⅲ的出口通过管路与所述冷箱相连通，且从所述冷箱引出后经节流与所述再冷凝器相连通，从所述再冷凝器引出后再进入至所述冷箱，最后从所述冷箱引出后与所述一级氮气压缩机相连通。
本发明提供的系统可用于原料气中甲烷含量在30～90%（体积分数）混空煤层气的液化。预处理合格后的原料气进入冷箱经冷却降温后进入精馏塔进行脱氧、脱氮，脱除杂质气的液相天然气再进入深冷单元又进一步降温，最后经过节流进入LNG储罐。混合冷剂循环机构通过压缩机将混合冷剂压缩、冷却后引入冷箱为天然气提供冷量，氮气冷剂循环机构通过压缩机将混合冷剂压缩、冷却后冷箱，液化后节流为精馏塔及天然气提供冷量。其中的混合冷剂可由一定配比的甲烷、乙烯、丙烷、氮气、异戊烷等组成。
本发明具有如下有益效果：
（1）本发明可实现原料气甲烷含量在30～90%混空煤层气的液化，减少碳排放，最大限度回收天然气资源；
（2）本发明采用混合冷剂+氮气循环，装置具备换热效率高，能耗低；
（3）本发明可以充分利用工艺流程中的冷量回收，降低系统能耗；
（4）使用本发明进行煤层气脱氧、氮精度高，甲烷回收率高等特点；
（5）本发明充分考虑国产设备的适用性，提高流程控制的自动化，减少系统开车时间；
（6）利用本发明进行液化后的LNG纯度高，便于运输。
附图说明
图1为本发明的含氧煤层气的脱氧、脱氮系统的示意图。
图中各标记如下：
CB1冷箱，C1-1一级混合冷剂压缩机、C1-2二级混合冷剂压缩机、C2-1一级氮气压缩机、C2-2二级氮气压缩机、C2-3三级氮气压缩机、V1-1混合冷剂气液分离器Ⅰ、V1-2混合冷剂气液分离器Ⅱ、V2精馏塔塔顶气液分离器、E1-1混合冷剂冷却器Ⅰ、E1-2混合冷剂冷却器Ⅱ、E2-1氮气冷却器Ⅰ、E2-2氮气冷却器Ⅱ、E2-3氮气冷却器Ⅲ、E3再冷凝器、E4再沸器，T1精馏塔。
具体实施方式
下面结合附图对本发明做进一步说明，但本发明并局限于以下实施例。
下述实施例中所使用的实验方法如无特殊说明，均为常规方法。
下述实施例中所用的材料、试剂等，如无特殊说明，均可从商业途径得到。
如图1所示，本发明提供的含氧煤层气脱氧、脱氮系统包括冷箱CB1、精馏塔T1、煤层气脱氧、脱氮机构、混合冷剂循环机构和氮气冷剂循环机构；该系统中，混合冷剂循环机构为冷箱CB1提供冷量，氮气冷剂循环机构为冷箱CB1和精馏塔T1提供冷量。本发明中，该煤层气脱氧、脱氮机构包括原料气管线（图中未标）、设置于精馏塔T1塔顶的再冷凝器E3和设置于精馏塔T1塔底的再沸器E4；其中的原料气管线与冷箱CB1相连通，然后从冷箱CB1中引出后与再沸器E4相连通；该原料气管线从再沸器E4引出后再进入至冷箱CB1中，然后从冷箱CB1中引出后与精馏塔T1相连通；该再沸器E4的气相出口通过管路与冷箱CB1相连通，该管路经冷箱CB1冷却后与LNG储罐相连通。
如图1所示，本发明中的混合冷剂循环机构为二级压缩单元，其包括一级混合冷剂压缩机C1-1、二级混合冷剂压缩机C1-2、混合冷剂冷却器ⅠE1-1、混合冷剂冷却器ⅡE1-2、混合冷剂气液分离器ⅠV1-1和混合冷剂气液分离器ⅡV1-2；其中一级混合冷剂压缩机C1-1的出口与混合冷剂冷却器ⅠE1-1相连通，混合冷剂冷却器ⅠE1-1的出口与混合冷剂气液分离器ⅠV1-1相连通；混合冷剂气液分离器ⅠV1-1的气相出口与二级混合冷剂压缩机C1-2的入口相连通，二级混合冷剂压缩机C1-2的出口与混合冷剂冷却器ⅡE1-2相连通，混合冷剂冷却器ⅡE1-2的出口和混合冷剂气液分离器ⅠV1-1的液相出口均与混合冷剂气液分离器ⅡV1-2相连通；该混合冷剂气液分离器ⅡV1-2的气相出口和液相出口均与冷箱CB1相连通，并进行节流，然后从冷箱CB1中引出后与一级混合冷剂压缩机C1-1相连通。
如图1所示，本发明中氮气冷剂循环机构为三级压缩单元，其包括依次连通的一级氮气压缩机C2-1、氮气冷却器ⅠE2-1、二级氮气压缩机C2-2、氮气冷却器ⅡE2-2、三级氮气压缩机C2-3和氮气冷却器ⅢE2-3；其中氮气冷却器ⅢE2-3的出口通过管路与冷箱CB1相连通，且从冷箱CB1引出后经节流与再冷凝器E3相连通，从再冷凝器E3引出后再进入至冷箱CB1中，最后从冷箱CB1引出后与一级氮气压缩机C2-1相连通。
下面以某一组成的煤层气为例，说明本发明系统的使用过程：
将煤矿抽采的煤层气液化，原料气组分体积分数为甲烷40%、氮气47.4%和氧气12.6%。
主要实施步骤如下：
本实施例采用的混合冷剂由19.28%氮气、42.73%甲烷、14.53%乙烯、9.39%丙烷、14.08%异戊烷组成（体积分数）。从冷箱换热后的混合冷剂进入一级混合冷剂压缩机C1-1经第一级压缩至1.5MPag后，进入混合冷剂冷却器ⅠE1-1至38℃后进入混合冷剂气液分离器ⅠV1-1，气相进入二级混合冷剂压缩机C1-2经第二级压缩至5.0MPag，然后经过混合冷剂冷却器ⅡE1-2冷却至38℃后进入混合冷剂分离器ⅡV1-2，混合冷剂气液分离器ⅠV1-1的液相经过泵P1-2泵入混合冷剂分离器ⅡV1-2；混合冷剂分离器ⅡV1-2的气相和液相混合均布后进入冷箱CB1，冷却到-160℃后节流到0.4MPag，返回冷箱为深冷、液化、预冷段提供冷量，复热至36℃返回一级混合冷剂压缩机C1-1入口缓冲罐，完成混合冷剂循环。
冷剂氮气经过三级压缩至5.53MPaA后进入氮气冷却器ⅢE2-3冷却至38℃，然后进入冷箱CB1冷却至-175℃后，引出冷箱节流后进入精馏塔T1顶部再冷凝器E3为再冷凝器提供冷量，然后返回冷箱CB1为冷箱过冷段、深冷段、液化段、预冷段提供冷量，复热至33℃后返回至氮气压缩机入口缓冲罐，完成氮气循环。
原料气采用低压，经预处理合格的原料气压力约0.4MPaA，进入冷箱CB1预冷至-54℃后，进入与精馏塔T1相连通的再沸器E4，出再沸器E4被冷却至-138℃后进入冷箱CB1液化段被冷却到-160℃后，进入精馏塔T1中进行精馏，从精馏塔T1相连接的再沸器E4出来的LNG温度约为-146℃，进入冷箱CB1进一步过冷至-158℃节流后进入储罐储存。

Claims (5)

1.一种含氧煤层气的脱氧、脱氮系统，其特征在于：所述系统包括冷箱、精馏塔、煤层气脱氧、脱氮机构、混合冷剂循环机构和氮气冷剂循环机构；
所述混合冷剂循环机构为所述冷箱提供冷量；
所述氮气冷剂循环机构为所述冷箱和所述精馏塔提供冷量；
所述煤层气脱氧、脱氮机构包括原料气管线、设置于所述精馏塔塔顶的再冷凝器和设置于所述精馏塔塔底的再沸器；所述原料气管线与所述冷箱相连通，然后从所述冷箱中引出后与所述再沸器相连通；所述原料气管线从所述再沸器引出后再进入至所述冷箱中，然后从所述冷箱中引出后与所述精馏塔相连通；所述再沸器的气相出口通过管路与所述冷箱相连通，所述管路经所述冷箱冷却后与LNG储罐相连通。
2.根据权利要求1所述的脱氧、脱氮系统，其特征在于：所述混合冷剂循环机构为二级压缩单元。
3.根据权利要求2所述的脱氧、脱氮系统，其特征在于：所述二级压缩单元包括一级混合冷剂压缩机、二级混合冷剂压缩机、混合冷剂冷却器Ⅰ、混合冷剂冷却器Ⅱ、混合冷剂气液分离器Ⅰ和混合冷剂气液分离器Ⅱ；
所述一级混合冷剂压缩机的出口与所述混合冷剂冷却器Ⅰ相连通，所述混合冷剂冷却器Ⅰ的出口与所述混合冷剂气液分离器Ⅰ相连通；所述混合冷剂气液分离器Ⅰ的气相出口与所述二级混合冷剂压缩机的入口相连通，所述二级混合冷剂压缩机的出口与所述混合冷剂冷却器Ⅱ相连通，所述混合冷剂冷却器Ⅱ的出口和所述混合冷剂气液分离器Ⅰ的液相出口均与所述混合冷剂气液分离器Ⅱ相连通；所述混合冷剂气液分离器Ⅱ的气相出口和液相出口均与所述冷箱相连通，并进行节流，然后从所述冷箱中引出后与所述一级混合冷剂压缩机相连通。
4.根据权利要求1-3中任一项所述的脱氧、脱氮系统，其特征在于：所述氮气冷剂循环机构为三级压缩单元。
5.根据权利要求4所述的脱氧、脱氮系统，其特征在于：所述三级压缩单元包括依次连通的一级氮气压缩机、氮气冷却器Ⅰ、二级氮气压缩机、氮气冷却器Ⅱ、三级氮气压缩机和氮气冷却器Ⅲ；
所述氮气冷却器Ⅲ的出口通过管路与所述冷箱相连通，且从所述冷箱引出后经节流与所述再冷凝器相连通，从所述再冷凝器引出后再进入至所述冷箱，最后从所述冷箱引出后与所述一级氮气压缩机相连通。
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