CN204298357U - 一种含氧煤层气脱氧、脱氮以及液化系统 - Google Patents

一种含氧煤层气脱氧、脱氮以及液化系统 Download PDF

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CN204298357U
CN204298357U CN201420468876.4U CN201420468876U CN204298357U CN 204298357 U CN204298357 U CN 204298357U CN 201420468876 U CN201420468876 U CN 201420468876U CN 204298357 U CN204298357 U CN 204298357U
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ice chest
nitrogen
rectifying column
pipeline
reboiler
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曾伟平
陈杰
尹全森
花亦怀
冯颉
李秋英
常心洁
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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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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Abstract

本实用新型公开了一种含氧煤层气脱氧、脱氮液化系统。所述液化系统包括冷箱、精馏塔、煤层气脱氧、脱氮机构和氮气冷剂循环机构；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。本实用新型实现了排放气中甲烷的高回收率；精馏塔的再沸器采用温度控制，保证含氧煤层气中氮气、氧气脱除的高精度。

Description

一种含氧煤层气脱氧、脱氮以及液化系统
技术领域
本实用新型涉及一种含氧煤层气脱氧、脱氮以及液化系统，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。2013年我国井下抽采煤层气126亿方，利用量约43亿方，利用量不足35％。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，例如中国专利申请200610080889.4，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。中国专利200610103425.0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，单一的混合冷剂制冷或透平膨胀所能达到的制冷温度不能满足高精度脱除煤层气中氮气、氧气的要求，使得排放其中甲烷含量较高，存在一定的安全问题，也降低了分离和液化的处理能力。而中国专利20101028282232.2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。
中国专利200910012669.1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。
实用新型内容
本实用新型的目的是提供一种含氧煤层气脱氧、脱氮以及液化系统，本实用新型液化系统采用冷剂氮气膨胀与节流制冷结合的方式，充分利用工艺流程中的冷量回收，同时保证甲烷回收率，具备换热效率高，能耗低，煤层气脱氧、氮精度高，甲烷回收率高，安全性高等特点。
本实用新型所提供的含氧煤层气脱氧、脱氮液化系统，包括冷箱、精馏塔、煤层气脱氧、脱氮机构和氮气冷剂循环机构；
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。
上述的含氧煤层气脱氧、脱氮液化系统中，所述氮气冷剂循环机构为三级压缩单元。
上述的含氧煤层气脱氧、脱氮液化系统中，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的出口通过管路与氮气膨胀机压缩端相连通，经压缩并冷却后出口通过管路与所述冷箱相连通，且从所述冷箱引出一部分氮气进入所述氮气膨胀压缩机膨胀端膨胀接口后与所述冷箱连通，从所述冷箱引出后与氮气压缩机二级入口缓冲罐相连通；另外一部分氮气经所述冷箱过冷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一级入口缓冲罐相连通。
本实用新型液化系统中，进入冷箱后的冷剂氮气一部分从冷箱中引出进入膨胀压缩机膨胀端膨胀，膨胀后的氮气返回冷箱，为冷箱深冷段、液化段和预冷段提供冷量，复热后返回冷剂氮气压缩机二级入口；另外一部分冷剂氮气经继续过冷后为液相，节流后进入精馏塔顶部的再冷凝器，为再冷凝器提供冷量后返回冷箱，为冷箱过冷段、深冷段、液化段和预冷段提供冷量，复热后返回冷剂氮气压缩机一级入口，完成一个冷剂氮气循环。
本实用新型液化系统中，液相氮气冷剂节流阀采用温度和流量的串级控制，实现了排放气中甲烷的高回收率；精馏塔的再沸器采用温度控制，保证含氧煤层气中氮气、氧气脱除的高精度；LNG产品节流阀采用温度和流量的串级控制，实现了目标装置冷热负荷匹配，装置平稳运行。冷剂压缩采用变频电机驱动，装置运行范围广。氮气循环具有快速启停，操作方便的优点。
附图说明
图1为实用新型含氧煤层气的脱氧、脱氮液化系统的示意图。
图中各标记如下：
CB-1冷箱，C1-1一级氮气压缩机、C1-2二级氮气压缩机、C1-3三级氮气压缩机、TE-1氮气膨胀压缩机、V-1～V-4冷剂氮气缓冲罐，V2精馏塔塔顶气液分离器、E-1～E-4冷剂氮气冷却器、E-5精馏塔塔顶冷凝器，E-6精馏塔塔底再沸器，T-1精馏塔、E-1～E-3氮气冷却器。
具体实施方式
下面结合附图对本实用新型做进一步说明，但本实用新型并不局限于以下实施例。
如图1所示，本实用新型提供的含氧煤层气脱氧、脱氮液化系统包括冷箱CB-1、精馏塔T-1、煤层气脱氧、脱氮机构和氮气冷剂循环机构；该系统中，氮气冷剂循环机构为冷箱CB-1和精馏塔T-1提供冷量。本实用新型中，该煤层气脱氧、脱氮机构包括原料气管线(图中未标)、设置于精馏塔塔顶冷凝器E-5和设置于精馏塔塔底再沸器E-6；其中的原料气管线与冷箱CB-1相连通，然后从冷箱CB-1中引出后与精馏塔塔底再沸器E-6相连通；该原料气管线从精馏塔塔底再沸器E-6引出后再进入至冷箱CB-1中，然后从冷箱CB-1中引出后与精馏塔T-1相连通；该精馏塔塔底再沸器E-6的气相出口通过管路与冷箱CB-1相连通，该管路经冷箱CB-1冷却后与LNG储罐相连通。
如图1所示，本实用新型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C1-1、氮气冷却器E-1、冷剂氮气缓冲罐V-1、二级氮气压缩机C1-2、氮气冷却器E-2、冷剂氮气缓冲罐V-2、三级氮气压缩机C1-3、氮气冷却器E1-3和～冷剂氮气缓冲罐V-3；最后与氮气膨胀压缩机TE-1压缩端相连通。经压缩单元压缩后的氮气经冷却器E-4冷却后进入冷箱CB-1中，经冷却后的一部分氮气从冷箱CB-1中引出，进入氮气膨胀压缩机TE-1的膨胀端，膨胀后的氮气返回冷箱CB-1为液化段、预冷段提供冷量，复热后与二级氮气压缩机C1-2的入口相联通；另外一部分氮气继续经冷箱CB-1过冷，过冷后从冷箱CB-1引出后经节流与精馏塔塔顶冷凝器E-5相连通，从精馏塔塔顶冷凝器E-5引出后再进入至冷箱CB-1中，最后从冷箱CB-1引出后与一级氮气压缩机C1-1相连通。
下面以某一组成的煤层气为例，说明本实用新型系统的使用过程：
将煤矿抽采的煤层气进行液化，原料气组成(体积)为：甲烷40％，氮气47.4％，氧气12.6％。采用冷剂为氮气。
经节流后的氮气经过精馏塔塔顶冷凝器E-5、冷箱CB-1换热后进入氮气压缩机经第一级压缩至0.475MPag后，进入冷却器E-1至38℃后，与膨胀后经冷箱CB-1复温返回的另一部分氮气冷剂混合进入氮气压缩机二级缓冲罐V-1，然后进入氮气压缩机第二级压缩至2.1MPag，然后经过冷却器E-2冷却至38℃后进入缓冲罐V-2，然后进入氮气压缩机第三级压缩至5.9MPag，然后经过冷却器E-3冷却至38℃后进入缓冲罐V-3，在经过氮气膨胀压缩机TE-1压缩端压缩机后，经冷却器E-4冷却至38℃，进入冷箱CB-1。
冷剂氮气进入冷箱CB-1经冷箱预冷、液化段冷却至-90℃，一部分冷剂氮气进入TE-1氮气膨胀机，膨胀节流到0.53MPaG，返回冷箱CB-1为深冷、液化、预冷段提供冷量，复热至-6℃返回氮气压缩机二级入口冷剂氮气缓冲罐V-2；另外一部分冷剂氮气经冷箱深冷段、过冷段冷却至-174℃节流，节流至0.233MPaG后进入精馏塔塔顶冷却E-5，为塔顶冷却器提供冷量，然后返回冷箱CB-1，为冷箱过冷段、深冷段、液化段、预冷段提供冷量，复热至-6℃返回氮气压缩机一级入口缓冲罐，经压缩机一级压缩后，与膨胀后氮气混合进入压缩机二级，完成冷剂氮气循环。
原料气采用低压，经预处理合格的原料气(经过脱硫、脱碳、脱汞和脱水处理，二氧化碳含量小于50ppmV，水含量小于1ppmV，H2S小于4ppmV)压力约0.4MPaA，经过预冷至0℃，预冷冷量由一套冷水机组提供，然后进入冷箱CB1预冷至-51℃后，进入精馏塔再沸器E-6，出精馏塔再沸器E-6被冷却至-135℃后进入冷箱CB-1液化段被冷却到-160℃后，进入精馏塔T-1精馏，从精馏塔再沸器E-6出来的LNG温度约为-146℃，进入冷箱CB-1进一步过冷至-158℃节流后进入储罐储存。
从精馏塔顶部分离出来的氮气、氧气排放气返回冷箱CB-1回收冷量后排放，排放气中甲烷含量小于1％。
LNG产品中甲烷含量为大于99.9％，氧气含量小于0.1％，氮气含量小于0.01％。

Claims (1)

1.一种含氧煤层气脱氧、脱氮液化系统，其特征在于：所述液化系统包括冷箱、精馏塔、煤层气脱氧、脱氮机构和氮气冷剂循环机构；
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；
所述氮气冷剂循环机构为三级压缩单元；
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的出口通过管路与氮气膨胀机压缩端相连通，经压缩并冷却后出口通过管路与所述冷箱相连通，且从所述冷箱引出一部分氮气进入所述氮气膨胀压缩机膨胀端膨胀接口后与所述冷箱连通，从所述冷箱引出后与所述氮气压缩机二级入口缓冲罐相连通；另外一部分氮气经所述冷箱过冷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氮气压缩机一级入口吸入罐相连通。
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CN105444527A (zh) * 2015-12-02 2016-03-30 中国石油大学(北京) 一种天然气处理装置及方法
CN107548446A (zh) * 2015-05-04 2018-01-05 通用电气石油和天然气公司 制备供存储的烃流
CN108826831A (zh) * 2018-08-24 2018-11-16 杭州中泰深冷技术股份有限公司 氮循环制冷的深冷分离一氧化碳气体的装置和工艺

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CN107548446A (zh) * 2015-05-04 2018-01-05 通用电气石油和天然气公司 制备供存储的烃流
US10928128B2 (en) 2015-05-04 2021-02-23 GE Oil & Gas, Inc. Preparing hydrocarbon streams for storage
US11988445B2 (en) 2015-05-04 2024-05-21 GE Oil & Gas, Inc. Preparing hydrocarbon streams for storage
CN105444527A (zh) * 2015-12-02 2016-03-30 中国石油大学(北京) 一种天然气处理装置及方法
CN105444527B (zh) * 2015-12-02 2017-10-03 中国石油大学(北京) 一种天然气处理装置及方法
CN108826831A (zh) * 2018-08-24 2018-11-16 杭州中泰深冷技术股份有限公司 氮循环制冷的深冷分离一氧化碳气体的装置和工艺
CN108826831B (zh) * 2018-08-24 2023-09-29 杭州中泰深冷技术股份有限公司 氮循环制冷的深冷分离一氧化碳气体的装置和工艺

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