CN105571269A - 含高氮氧氢的煤层气低温精馏液化分离回收系统及方法 - Google Patents

含高氮氧氢的煤层气低温精馏液化分离回收系统及方法 Download PDF

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CN105571269A
CN105571269A CN201510941417.2A CN201510941417A CN105571269A CN 105571269 A CN105571269 A CN 105571269A CN 201510941417 A CN201510941417 A CN 201510941417A CN 105571269 A CN105571269 A CN 105571269A
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CN105571269B (zh
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花亦怀
陈杰
褚洁
苏清博
杨文刚
尹全森
浦晖
鹿来运
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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

本发明涉及一种含高氮氧氢的煤层气低温精馏液化分离回收系统及方法，设置一包括冷箱、重烃分离罐、精馏塔、LCPM储罐、冷剂压缩机、冷却器、末级气液分离器、闪蒸气压缩机及闪蒸气冷却器的含高氮氧氢的煤层气低温精馏液化分离回收系统；原料气经冷箱预冷段预冷后进行重烃分离、液化；液化后进入精馏塔脱除氮氢氧气后返回冷箱继续降温后进入LCPM储罐；混合冷剂气体经过两级压缩及冷却后，经末级气液分离器分离后的液相冷剂为冷箱预冷段提供冷量；分离后的气相冷剂为冷箱液化和过冷段提供冷量；弛放气被加热后放空；闪蒸气与液相冷剂换热后增压返回冷箱液化段进行再液化。本发明能提高甲烷回收率，从而提高装置处理能力，降低系统能耗，节约生产成本。

Description

含高氮氧氢的煤层气低温精馏液化分离回收系统及方法
技术领域
本发明涉及一种分离原料气中氮氧氢的系统及方法，特别是关于一种利用液化原理的含高氮氧氢的煤层气低温精馏液化分离回收系统及方法。
背景技术
我国煤层气资源丰富，国家不断出台政策促进煤层气产业的发展，提高煤层气资源的利用率。煤层气主要成为是甲烷，是比较重要的能源和化工燃料。煤层气中成分复杂，大部分煤层气由于加工处理技术的限制没有被合理利用，工业应用较少，大部分煤层气直接放空，不仅造成了资源的浪费，而且还会严重污染大气环境。
针对煤层气的利用目前主要是开采后运用管网进行输送。随着液化技术的发展，煤层气液化项目日趋增多，利用液化技术将煤层气与空气分离液化，方便运输和存储。目前，关于煤层气液化方向出现了多种技术，申请号为200610103425.0的文献中公开了一种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、装置结构简单等优点，但是该工艺采用混合制冷或膨胀制冷等常规的制冷方式，结构复杂，制冷效率较低，降低了分离和液化装置的处理能力；申请号为200610080889.4的文献中公开了一种含空气煤层气液化工艺及设备，采用低温双级精馏方法，分离纯度高，但工艺复杂，能耗较高；申请号为201110319450.3的文献中公开了一种煤层气液化方法及煤层气液化系统，内容为煤层气从原料气出井到罐装储运的过程，考虑了物质和能量的回收利用，但是并没有公开具体液化工艺以及脱除煤层气中杂质的技术方法。
发明内容
针对上述问题，本发明的目的是提供一种含高氮氧氢的煤层气低温精馏液化分离回收系统及方法，其涵盖原料气液化、低温精馏、制冷循环、驰放气处理及闪蒸气利用等过程，充分并有效利用工艺中冷量回收过程提高制冷效率，提高甲烷回收率，从而提高装置处理能力，降低系统能耗，节约生产成本。
为实现上述目的，本发明采取以下技术方案：一种含高氮氧氢的煤层气低温精馏液化分离回收方法，其特征在于，该方法其步骤如下：1)设置一包括冷箱、重烃分离罐、精馏塔、LCPM储罐、冷剂压缩机、冷却器、末级气液分离器、闪蒸气压缩机及闪蒸气冷却器的含高氮氧氢的煤层气低温精馏液化分离回收系统；2)原料气液化过程：预处理合格的原料气经冷箱预冷段预冷后进行重烃分离，重烃脱除后的原料气分为两路：一路返回冷箱液化段继续降温；另一路为精馏塔底再沸器提供热量，自身被冷却后返回冷箱液化段与第一股原料气汇合，直至被液化；3)低温精馏过程：液化后的原料气进入精馏塔，脱除氮、氢、氧气；LCPM返回冷箱过冷段继续降温直至过冷，经节流减压后进入LCPM储罐；4)制冷循环过程：来自冷箱的混合冷剂气体经过冷剂压缩机两级压缩及冷却器冷却后形成气液两相流体，经末级气液分离器分离后的液相冷剂为冷箱预冷段提供冷量；分离后的气相冷剂为冷箱液化和过冷段提供冷量；5)弛放气处理过程：来自精馏塔塔顶气液分离罐的弛放气被加热后，放空至火炬；6)闪蒸气利用：来自LCPM储罐的闪蒸气与液相冷剂换热后进入闪蒸气压缩机，增压后的闪蒸气回收弛放气冷量后返回冷箱液化段进行再液化处理。
一种实现上述方法的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述系统包括冷箱、精馏塔、脱氮、氢、氧气系统、冷剂循环系统、驰放气处理系统和闪蒸气利用系统；所述脱氮、氢、氧气系统包括原料气管线、精馏塔、重烃分离罐、冷凝器和再沸器；所述冷凝器设置在所述精馏塔塔顶，所述再沸器设置在所述精馏塔塔底；所述原料气管线与所述冷箱预冷段连通，所述原料气管线由所述冷箱引出后与所述重烃分离罐连通，该原料气管线从所述重烃分离罐气相出口引出后分为两路：一路进入所述冷箱液化段的中温段，另一路与所述再沸器连通；该原料气管线从所述再沸器引出后进入所述冷箱液化段的低温段，从所述冷箱中引出的原料气管线与所述精馏塔连通；所述再沸器液相出口通过所述原料气管线与所述冷箱连通，经所述冷箱冷却直至过冷，然后该原料气管线与所述LCPM储罐连通；所述冷剂循环系统包括冷剂压缩机单元和冷剂管线，所述冷剂压缩机单元包括一级冷剂压缩机、二级冷剂压缩机、级间冷却器、末级冷却器和末级气液分离器；所述一级冷剂压缩机出口经所述级间冷却器与所述二级冷剂压缩机的入口连通，所述二级冷剂压缩机出口经所述末级冷却器与所述末级气液分离器连通；由所述末级气液分离器气相出口引出的冷剂管线与所述冷箱预冷段连通，所述冷剂管线从所述冷箱底部过冷段中引出后分为两路：一路进入所述冷凝器中提供冷量，然后返回所述冷箱过冷段；另一路节流后返回所述冷箱过冷段；由所述末级气液分离器液相出口引出的冷剂管线与所述闪蒸气换热器连通，所述冷剂管线从所述闪蒸气换热器引出后再进入所述冷箱预冷段中，从所述冷箱液化段引出后返回所述冷箱液化段；所述冷剂管线从所述冷箱预冷段引出后与所述一级冷剂压缩机入口连通；所述驰放气处理系统包括驰放气管线、设置于所述精馏塔塔顶的气液分离罐和驰放气换热器；所述驰放气管线从所述冷凝器中引出后与所述气液分离罐连通，所述驰放气管线从所述气液分离罐气相出口引出后进入所述驰放气换热器；所述闪蒸气利用系统包括闪蒸气管线、闪蒸气换热器和闪蒸气压缩单元，所述闪蒸气压缩单元包括一级闪蒸气压缩机和闪蒸气冷却器；所述闪蒸气管线从所述LCPM储罐中引出后与所述闪蒸气换热器连通，闪蒸气在所述闪蒸气换热器中换热至常温后与所述一级闪蒸气压缩机入口连通，所述一级闪蒸气压缩机出口与所述闪蒸气冷却器连通；所述闪蒸气管线从所述闪蒸气冷却器引出后分为两路：一路进入原料气管线用作原料气，另一路与所述驰放气换热器连接，与来自所述气液分离罐的驰放气进行换热后从所述驰放气换热器引出，进入所述冷箱液化段，从所述冷箱过冷段引出后与所述LCPM储罐连通。
所述脱氮、氢、氧气系统中，在所述重烃分离罐顶部气相出口与所述冷箱预冷段连接的原料气管线上设置有第一阀门，在所述重烃分离罐底部液相出口原料气管线上设置有第二阀门，在所述冷箱过冷段与所述精馏塔连接的原料气管线上设置有第三阀门，在所述再沸器热端出口与所述冷箱液化段连接的原料气管线上设置有第四阀门，在从所述冷箱过冷段引出的所述原料气管线与所述LCPM储罐连接的管线上设置有第五阀门。
所述冷剂循环系统中，在所述冷剂管线从所述冷箱预冷段引出后再返回所述冷箱液化段之间的管线上设置有第六阀门，在所述冷剂管线从所述冷箱过冷段引出后再返回所述冷箱过冷段之间的管线上设置有第七阀门，在所述冷箱过冷段与所述冷凝器连接管线上设置有第八阀门。
所述驰放气处理系统中，在所述气液分离罐与所述驰放气换热器连接的管线上设置有第九阀门。
所述闪蒸气利用系统中，在从所述冷箱过冷段引出的所述闪蒸气管线与所述LCPM储罐连接的管线上设置有第十阀门，在所述LCPM储罐顶部出口与所述闪蒸气换热器连接的管线上设置有第十一阀门，在从所述闪蒸气冷却器引出的闪蒸气管线去往燃料气系统的管线上设置有第十二阀门。
所述冷箱、重烃分离罐、气液分离罐、末级气液分离器、精馏塔和LCPM储罐内均设置有压力测量指示装置。
所述冷箱、精馏塔、冷凝器、再沸器、级间冷却器、末级冷却器、闪蒸气换热器、闪蒸气冷却器和驰放气换热器入口及出口均设置有温度检测指示装置。
所述重烃分离罐、气液分离罐、末级气液分离器、所述精馏塔、LCPM储罐和再沸器内均设置有液位控制仪表。
本发明由于采取以上技术方案，其具有以下优点：1、本发明能有效回收天然气资源，减少废气排放造成污染。2、本发明采用合理充分的回收利用冷量，提高制冷效率，降低系统能耗。3、本发明充分回收利用闪蒸气，提高系统的液化率，有效提高液化煤层气产量，节约生产成本。4、本发明提供的脱氮氧氢工艺，具有甲烷回收率高，脱氮氧氢精度高，驰放气甲烷排放量低等特点。5、本发明可用于煤层气液化工厂，工艺流程自动化控制水平高，具有很强的可操作性和工艺适应能力；液化煤层气(LCPM)纯度高，同时便于装车外输。
附图说明
图1是本发明的系统整体结构示意图。
具体实施方式
下面结合附图和实施例对本发明进行详细的描述。
如图1所示，本发明提供一种含高氮氧氢的煤层气低温精馏液化分离回收系统，其包括冷箱E1、精馏塔T2、脱氮、氢、氧气系统、冷剂循环系统、驰放气处理系统和闪蒸气利用系统；其中，冷剂循环系统为冷箱E1和精馏塔T2提供冷量。
脱氮、氢、氧气系统包括原料气管线、精馏塔T2、重烃分离罐V1、冷凝器E2、再沸器E8和阀门1至阀门5；其中，冷凝器E2设置在精馏塔T2塔顶，再沸器E8设置在精馏塔T2塔底。原料气管线与冷箱E1预冷段连通，原料气管线由冷箱E1引出后与重烃分离罐V1连通，重烃分离罐V1底部液相出口管线上设置有阀门2，该原料气管线从重烃分离罐V1气相出口引出后分为两路：一路经过阀门1后进入冷箱E1液化段的中温段，使原料气继续降温；另一路与再沸器E8连通。该原料气管线从再沸器E8热端出口引出后，经过阀门4进入冷箱E1液化段的低温段，与第一路原料气汇合继续降温直至液化，然后从冷箱E1中引出，引出的原料气管线经过阀门3将原料气节流减压至20-30bar后与精馏塔T2连通。再沸器E8液相出口通过原料气管线与冷箱E1连通，经冷箱E1冷却直至过冷，然后该原料气管线经过阀门5与LCPM储罐T1连通。
冷剂循环系统包括冷剂压缩机单元、冷剂管线和阀门6至阀门8；其中，冷剂压缩机单元包括一级冷剂压缩机C1-1、二级冷剂压缩机C1-2、级间冷却器E6、末级冷却器E7和末级气液分离器V3。一级冷剂压缩机C1-1出口经级间冷却器E6与二级冷剂压缩机C1-2的入口连通，二级冷剂压缩机C1-2出口经末级冷却器E7与末级气液分离器V3连通。由末级气液分离器V3气相出口引出的冷剂管线与冷箱E1预冷段连通，冷剂管线从冷箱E1底部过冷段中引出后分为两路：一路经过阀门8后进入冷凝器E2中，用于给精馏塔T2塔顶驰放气提供冷量，然后返回冷箱E1过冷段；另一路经过阀门7节流后返回冷箱E1过冷段。由末级气液分离器V3液相出口引出的冷剂管线与闪蒸气换热器E4连通，冷剂管线从闪蒸气换热器E4引出后再进入冷箱E1预冷段中，从冷箱E1液化段引出后，经过阀门6进行节流后返回冷箱E1液化段。冷剂管线从冷箱E1预冷段引出后与一级冷剂压缩机C1-1入口连通。
驰放气处理系统包括驰放气管线、设置于精馏塔T2塔顶的气液分离罐V2、驰放气换热器E3和阀门9。驰放气管线从冷凝器E2中引出后与气液分离罐V2连通，驰放气管线从气液分离罐V2气相出口引出后，经过阀门9进入驰放气换热器E3换热升温后，进入火炬系统。
闪蒸气利用系统包括闪蒸气管线、闪蒸气换热器E4、闪蒸气压缩单元和阀门10至阀门12，其中，闪蒸气压缩单元包括一级闪蒸气压缩机C2和闪蒸气冷却器E5。闪蒸气管线从LCPM储罐T1中引出后，经阀门11与闪蒸气换热器E4连通，闪蒸气在闪蒸气换热器E4中换热至常温后与一级闪蒸气压缩机C2入口连通，一级闪蒸气压缩机C2出口与闪蒸气冷却器E5连通。闪蒸气管线从闪蒸气冷却器E5引出后分为两路：一路经过阀门12调压后进入燃料气管线用作燃料气，另一路与驰放气换热器E3连接，与来自气液分离罐V2的驰放气进行换热后从驰放气换热器E3引出，然后进入冷箱E1液化段，从冷箱E1过冷段引出，经过阀门10节流后与LCPM储罐T1连通。
上述实施例中，冷箱E1、重烃分离罐V1、气液分离罐V2、末级气液分离器V3、精馏塔T2和LCPM储罐T1内均设置有压力测量指示装置。
上述各实施例中，冷箱E1、精馏塔T2、冷凝器E2、再沸器E8、级间冷却器E6、末级冷却器E7、闪蒸气换热器E4、闪蒸气冷却器E5和驰放气换热器E3入口及出口均设置有温度检测指示装置。
上述各实施例中，重烃分离罐V1、气液分离罐V2、末级气液分离器V3、所述精馏塔T2、LCPM储罐T1和再沸器E8内均设置有液位控制仪表。
本发明提供一种含高氮氧氢的煤层气低温精馏液化分离回收方法，其步骤如下：
1)原料气液化过程：预处理合格的原料气经冷箱E1预冷段预冷后进行重烃分离，重烃脱除后的原料气分为两路：一路返回冷箱E1液化段继续降温；另一路为精馏塔T2底再沸器提供热量，自身被冷却后返回冷箱E1液化段与第一股原料气汇合，直至被液化。
2)低温精馏过程：液化后的原料气进入精馏塔T2，脱除氮、氢、氧气。液化煤层气(LCPM)返回冷箱E1过冷段继续降温直至过冷，经节流减压后进入LCPM储罐T1。
3)制冷循环过程：来自冷箱E1的混合冷剂气体经过冷剂压缩机两级压缩及冷却器冷却后形成气液两相流体。经末级气液分离器V3分离后的液相冷剂为冷箱E1预冷段提供冷量；分离后的气相冷剂为冷箱E1液化和过冷段提供冷量。
4)弛放气处理过程：来自精馏塔T2塔顶气液分离罐V2的弛放气被加热后，放空至火炬。
5)闪蒸气利用：来自LCPM储罐T1的闪蒸气与液相冷剂换热后进入闪蒸气压缩机，增压后的闪蒸气回收弛放气冷量后返回冷箱E1液化段进行再液化处理。
上述各实施例仅用于说明本发明，各部件的结构、尺寸、设置位置及形状都是可以有所变化的，在本发明技术方案的基础上，凡根据本发明原理对个别部件进行的改进和等同变换，均不应排除在本发明的保护范围之外。

Claims (9)

1.一种含高氮氧氢的煤层气低温精馏液化分离回收方法，其特征在于，该方法其步骤如下：
1)设置一包括冷箱、重烃分离罐、精馏塔、LCPM储罐、冷剂压缩机、冷却器、末级气液分离器、闪蒸气压缩机及闪蒸气冷却器的含高氮氧氢的煤层气低温精馏液化分离回收系统；
2)原料气液化过程：预处理合格的原料气经冷箱预冷段预冷后进行重烃分离，重烃脱除后的原料气分为两路：一路返回冷箱液化段继续降温；另一路为精馏塔底再沸器提供热量，自身被冷却后返回冷箱液化段与第一股原料气汇合，直至被液化；
3)低温精馏过程：液化后的原料气进入精馏塔，脱除氮、氢、氧气；LCPM返回冷箱过冷段继续降温直至过冷，经节流减压后进入LCPM储罐；
4)制冷循环过程：来自冷箱的混合冷剂气体经过冷剂压缩机两级压缩及冷却器冷却后形成气液两相流体，经末级气液分离器分离后的液相冷剂为冷箱预冷段提供冷量；分离后的气相冷剂为冷箱液化和过冷段提供冷量；
5)弛放气处理过程：来自精馏塔塔顶气液分离罐的弛放气被加热后，放空至火炬；
6)闪蒸气利用：来自LCPM储罐的闪蒸气与液相冷剂换热后进入闪蒸气压缩机，增压后的闪蒸气回收弛放气冷量后返回冷箱液化段进行再液化处理。
2.一种实现如权利要求1所述方法的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述系统包括冷箱、精馏塔、脱氮、氢、氧气系统、冷剂循环系统、驰放气处理系统和闪蒸气利用系统；所述脱氮、氢、氧气系统包括原料气管线、精馏塔、重烃分离罐、冷凝器和再沸器；所述冷凝器设置在所述精馏塔塔顶，所述再沸器设置在所述精馏塔塔底；所述原料气管线与所述冷箱预冷段连通，所述原料气管线由所述冷箱引出后与所述重烃分离罐连通，该原料气管线从所述重烃分离罐气相出口引出后分为两路：一路进入所述冷箱液化段的中温段，另一路与所述再沸器连通；该原料气管线从所述再沸器引出后进入所述冷箱液化段的低温段，从所述冷箱中引出的原料气管线与所述精馏塔连通；所述再沸器液相出口通过所述原料气管线与所述冷箱连通，经所述冷箱冷却直至过冷，然后该原料气管线与所述LCPM储罐连通；
所述冷剂循环系统包括冷剂压缩机单元和冷剂管线，所述冷剂压缩机单元包括一级冷剂压缩机、二级冷剂压缩机、级间冷却器、末级冷却器和末级气液分离器；所述一级冷剂压缩机出口经所述级间冷却器与所述二级冷剂压缩机的入口连通，所述二级冷剂压缩机出口经所述末级冷却器与所述末级气液分离器连通；由所述末级气液分离器气相出口引出的冷剂管线与所述冷箱预冷段连通，所述冷剂管线从所述冷箱底部过冷段中引出后分为两路：一路进入所述冷凝器中提供冷量，然后返回所述冷箱过冷段；另一路节流后返回所述冷箱过冷段；由所述末级气液分离器液相出口引出的冷剂管线与所述闪蒸气换热器连通，所述冷剂管线从所述闪蒸气换热器引出后再进入所述冷箱预冷段中，从所述冷箱液化段引出后返回所述冷箱液化段；所述冷剂管线从所述冷箱预冷段引出后与所述一级冷剂压缩机入口连通；
所述驰放气处理系统包括驰放气管线、设置于所述精馏塔塔顶的气液分离罐和驰放气换热器；所述驰放气管线从所述冷凝器中引出后与所述气液分离罐连通，所述驰放气管线从所述气液分离罐气相出口引出后进入所述驰放气换热器；
所述闪蒸气利用系统包括闪蒸气管线、闪蒸气换热器和闪蒸气压缩单元，所述闪蒸气压缩单元包括一级闪蒸气压缩机和闪蒸气冷却器；所述闪蒸气管线从所述LCPM储罐中引出后与所述闪蒸气换热器连通，闪蒸气在所述闪蒸气换热器中换热至常温后与所述一级闪蒸气压缩机入口连通，所述一级闪蒸气压缩机出口与所述闪蒸气冷却器连通；所述闪蒸气管线从所述闪蒸气冷却器引出后分为两路：一路进入原料气管线用作原料气，另一路与所述驰放气换热器连接，与来自所述气液分离罐的驰放气进行换热后从所述驰放气换热器引出，进入所述冷箱液化段，从所述冷箱过冷段引出后与所述LCPM储罐连通。
3.如权利要求2所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述脱氮、氢、氧气系统中，在所述重烃分离罐顶部气相出口与所述冷箱预冷段连接的原料气管线上设置有第一阀门，在所述重烃分离罐底部液相出口原料气管线上设置有第二阀门，在所述冷箱过冷段与所述精馏塔连接的原料气管线上设置有第三阀门，在所述再沸器热端出口与所述冷箱液化段连接的原料气管线上设置有第四阀门，在从所述冷箱过冷段引出的所述原料气管线与所述LCPM储罐连接的管线上设置有第五阀门。
4.如权利要求2所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述冷剂循环系统中，在所述冷剂管线从所述冷箱预冷段引出后再返回所述冷箱液化段之间的管线上设置有第六阀门，在所述冷剂管线从所述冷箱过冷段引出后再返回所述冷箱过冷段之间的管线上设置有第七阀门，在所述冷箱过冷段与所述冷凝器连接管线上设置有第八阀门。
5.如权利要求2至4任一项所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述驰放气处理系统中，在所述气液分离罐与所述驰放气换热器连接的管线上设置有第九阀门。
6.如权利要求2至4任一项所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述闪蒸气利用系统中，在从所述冷箱过冷段引出的所述闪蒸气管线与所述LCPM储罐连接的管线上设置有第十阀门，在所述LCPM储罐顶部出口与所述闪蒸气换热器连接的管线上设置有第十一阀门，在从所述闪蒸气冷却器引出的闪蒸气管线去往燃料气系统的管线上设置有第十二阀门。
7.如权利要求2至4任一项所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述冷箱、重烃分离罐、气液分离罐、末级气液分离器、精馏塔和LCPM储罐内均设置有压力测量指示装置。
8.如权利要求2至4任一项所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述冷箱、精馏塔、冷凝器、再沸器、级间冷却器、末级冷却器、闪蒸气换热器、闪蒸气冷却器和驰放气换热器入口及出口均设置有温度检测指示装置。
9.如权利要求2至4任一项所述的含高氮氧氢的煤层气低温精馏液化分离回收系统，其特征在于：所述重烃分离罐、气液分离罐、末级气液分离器、所述精馏塔、LCPM储罐和再沸器内均设置有液位控制仪表。
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