CN102653692A - 焦炉煤气制取液化天然气的方法 - Google Patents

焦炉煤气制取液化天然气的方法 Download PDF

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CN102653692A
CN102653692A CN2012101607328A CN201210160732A CN102653692A CN 102653692 A CN102653692 A CN 102653692A CN 2012101607328 A CN2012101607328 A CN 2012101607328A CN 201210160732 A CN201210160732 A CN 201210160732A CN 102653692 A CN102653692 A CN 102653692A
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coke
oven gas
coke oven
oven
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CN102653692B (zh
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唐令力
陈杰
单彤文
尹全森
王秀林
邰晓亮
杨文刚
浦晖
常心洁
陈海平
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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

本发明公开了一种焦炉煤气制取液化天然气的方法。包括如下步骤：（1）将焦炉煤气原料气进行压缩冷却；（2）将经冷却后的焦炉煤气分成两股：焦炉煤气物流A和焦炉煤气物流B；所述焦炉煤气物流B经J-T阀节流降压和冷却后进入至气提塔塔底；（3）所述焦炉煤气物流A经冷却后进入至气液分离罐中；所述气液分离罐的底部出来的液体物流进入气提塔；所述气提塔塔底的物流经J-T阀节流即得液化天然气；所述冷却均在换热器中进行。本发明提供的方法，能直接将焦炉气分离出合格的液化天然气产品，液化天然气可方便进行运输和利用，提高焦炉气的附加值；焦炉气回收工艺流程简单、自动化程度高，所采用的设备可靠，提高焦炉气回收装置的经济效益。

Description

焦炉煤气制取液化天然气的方法
技术领域
本发明涉及一种焦炉煤气制取液化天然气的方法。
背景技术
每年我国累计生产焦炭3~4亿吨，按吨焦产420m3焦炉煤气计算，焦炉煤气产量为1449亿m3。由于我国大多数钢铁企业的焦化厂使用高炉煤气加热焦炉，基本上焦炉煤气被全部利用，而独立的焦化厂约有一半的焦炉煤气用于焦炉自身加热，另外一半的焦炉煤气向外输送或设置专门的装置回收。预计全国的焦化企业每年至少向外输送或需要设置专门装置回收焦炉煤气的量为300亿m3，传统利用焦炉气生产甲醇，由于受市场等因素影响，目前甲醇市场供大于求，利用焦炉煤气生产甲醇的装置效益不高。如此大量的焦炉煤气，如何合理、高效、洁净利用，是一项十分紧迫的重要任务。
焦炉煤气中含有大量的H2、CH4、CO等可燃气体，如果将这些气体加以合理的利用，既可以缓解国内能源不足的现状，又可以为焦化企业带来良好的经济效益。
焦炉气若深度净化、甲烷化和脱水后可用来生产液化天然气（LNG），每年我国若回收300亿立方米放散的焦炉气，可得到约130亿立方米天然气，并减排大量的甲烷、SO2以及焦油、萘、氨等有害物质。因此，焦炉煤气制LNG项目不仅可有效缓解国内天然气短缺的问题，而且将促进焦化与能源行业的技术进步与产业发展，发展焦炉气制LNG项目产生较明显的经济效益、环境效益与社会效益，对于焦炉气回收利用产业具有重要意义。
焦炉煤气的典型组成如表1所示，其与常规天然气的组成有很大区别，其中氢、氮含量相对较高，相对与常规天然气，生产LNG产品能耗较高，液化工艺也更复杂。
表1焦炉煤气的典型组成
  组成V%   H2   CH4   CO   N2   CO2   CnHm   O2   热值Mj/Nm3
  含量   54~59   24~28   5.5~7   3~5   1~3   2~3   0.3~0.7   ~17
发明内容
本发明针对焦炉煤气中氢气、氮气含量较高，提供了一种焦炉煤气制取液化天然气的方法，该方法可以将焦炉煤气分离和液化，得到的液化天然气纯度可达到99%以上，液化和分离工艺简单、自动化程度高、操作方便，能够很好地解决焦炉煤气的回收问题。
本发明所提供的一种焦炉煤气制取液化天然气的方法，包括如下步骤：
（1）将焦炉煤气原料气进行压缩和冷却；
（2）将经冷却后的焦炉煤气分成两股：焦炉煤气物流A和焦炉煤气物流B；所述焦炉煤气物流B经J-T阀节流降压和冷却后进入至气提塔塔底；
（3）所述焦炉煤气物流A经冷却后进入至气液分离罐中；所述气液分离罐的底部出来的液体物流进入气提塔；所述气提塔塔底的物流经J-T阀节流即得液化天然气；
所述冷却均在换热器中进行。
上述的方法中，所述气液分离罐底部的物流从所述气提塔的顶部进入至所述气提塔中。
上述的方法中，所述焦炉煤气原料气经压缩冷却和预冷后进入重烃分离罐，用于分离焦炉气原料中可能含有的重烃类成分。
上述的方法中，步骤（2）中，将所述焦炉煤气物流B冷却至-120℃～-150℃，如-140℃；所述冷却过程为所述气提塔提供热量。
上述的方法中，步骤（3）中，将所述焦炉煤气物流A冷却至-140℃～-160℃，如-150℃。
上述的方法中，所述换热器组的冷量由制冷系统提供；所述制冷系统可选择混合冷剂制冷系统，也可选择气体膨胀制冷系统，所述制冷系统并不局限于某一种制冷系统。
上述的方法中，从所述气液分离罐的顶部出来的物流（主要为H2）经所述换热器复温。
上述的方法中，从所述气提塔塔顶出来的物流（主要为N2）经所述换热器复温。
上述的方法中，所述换热器具体可为板翅换热器或绕管式换热器。
本发明提供的方法，能直接将焦炉气分离出合格的液化天然气产品，液化天然气可方便进行运输和利用，提高焦炉气的附加值；焦炉气回收工艺流程简单、自动化程度高，所采用的设备可靠，提高焦炉气回收装置的经济效益。
附图说明
图1和图2均为本发明实施例1中混合制冷剂循环制取LNG的流程示意图；
图3为本发明实施例2中氮气膨胀制冷循环制取LNG的流程示意图。
具体实施方式
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。
实施例1、
本实施例采用二级节流的混合制冷剂循环、气提法制取LNG。
如图1所示，该工艺流程主要包括混合制冷剂液化系统、焦炉气冷却和氢气、氮气分离系统；其中混合制冷剂液化系统为混合制冷剂压缩和节流制冷系统，其包括混合制冷剂压缩机、水冷却器或空气冷却器、混合冷剂液体泵、板翅式换热器；焦炉气冷却和氢气、氮气分离系统包括重烃分离罐、气液分离罐和气提塔，气提塔不设置再沸器和过热器，简化塔器结构，通过控制气提塔底部气体流量，控制LNG的纯度。
其工艺流程如下：
如图1所示：将含H2、N2的净化合格的焦炉煤气经换热器E-100冷却后，进入至重烃分离罐V-103中进行重烃分离；然后气体天然气分两股物流A和B；焦炉煤气物流B先经J-T阀节流降压，达到气提塔的操作压力0.4MPa左右后进入换热器E-102中冷却的物流5的温度至-140℃左右后，为气提塔T-100提供热源；焦炉煤气物流A经换热器E-101冷却至-150℃左右后，进入气液分离罐V-100中，经气液分离罐分离出大部分H2后的液相物流1，经J-T阀节流降压后进入气提塔T-100的顶部，在气提塔内物流经过充分的质、热交换后，气提塔T-100顶部引出以氮气为主要成分的气体物流4，依次返回E-102、E-101和E-100中，温度复温到常温，为换热器提供冷量；气提塔T-100塔底部物流13经J-T阀节流得到高纯度的液态天然气。气液分离罐V-100分离出的气体物流2依次返回E-101和E-100中，物流3复温到常温。
低压的混合制冷剂物流7经过压缩机C-100和冷却器E-104压缩、冷却到常温后，为气液两相流体，进入气液分离器V-101分离为气体冷剂物流9和液体冷剂物流8，物流9和8分别经过C-101和P-100加压后汇合，进入冷却器E-105中冷却到常温的两相流体10，物流10进入气液分离器V-102中，分离出气体物流11和液体物流12。物流12经过换热器E-100冷却后，物流14温度达到-50℃左右，进行节流制冷，为换热器E-100提供冷量；物流11经过换热器E-100和E-101冷却后，物流15的温度达到-150℃左右，进行节流制冷，为换热器E-101提供冷量。
如图2所示：将含H2、N2的净化合格的焦炉煤气经换热器E-100冷却后，进入至重烃分离罐V-103中进行重烃分离；然后气体天然气分两股物流A和B；焦炉煤气物流B先经J-T阀节流降压，达到气提塔的操作压力0.4MPa左右后进入换热器E-102中冷却的物流5的温度至-140℃左右后，为气提塔T-100提供热源；焦炉煤气物流A经换热器E-101冷却至-150℃左右后，进入气液分离罐V-100中，经气液分离罐分离出大部分H2后的液相物流1，经J-T阀节流降压后进入气提塔T-100的顶部，在气提塔内物流经过充分的质、热交换后，气提塔T-100顶部引出以氮气为主要成分的气体物流4，依次返回E-102、E-101和E-100中，温度复温到常温，为换热器提供冷量；气提塔T-100塔底部物流11经J-T阀节流得到高纯度的液态天然气。气液分离罐V-100分离出的气体物流2依次返回E-101和E-100中，物流3复温到常温。
低压的混合制冷剂物流7经过压缩机C-100和冷却器E-104压缩、冷却到常温后，不产生冷凝液，气体物流8再经过压缩机C-101和冷却器E-105压缩、冷却到常温后为气液两相流体，两相流体的物流9依次经过换热器E-100和E-101冷却后，物流10的温度达到-150℃左右，进行节流制冷，为换热器E-101和E-100提供冷量。
实施例2、
本实施例为采用氮膨胀制冷、气提法制取LNG。
如图3所示，该工艺流程主要包括氮气膨胀制冷系统、焦炉气冷却和氢气、氮气分离系统；其中氮气膨胀制冷系统为氮气压缩机、冷却器、透平膨胀机，以及绕管式换热器；焦炉气冷却和氢气、氮气分离系统包括重烃分离罐、气液分离罐和气提塔，气提塔不设置再沸器和过热器，简化塔器结构，通过控制气提塔底部气体流量，控制LNG的纯度。
如图3所示：将含H2、N2的净化合格的焦炉煤气经换热器E-100冷却后，进入至重烃分离罐V-103中进行重烃分离；然后气体天然气分两股物流A和B；焦炉煤气物流B先经J-T阀节流降压，达到气提塔的操作压力0.4MPa左右后进入换热器E-102中冷却的物流5的温度至-140℃左右后，为气提塔T-100提供热源；焦炉煤气物流A经换热器E-101冷却至-150℃左右后，进入气液分离罐V-100中，经气液分离罐分离出大部分H2后的液相物流1，经J-T阀节流降压后进入气提塔T-100的顶部，在气提塔内物流经过充分的质、热交换后，气提塔T-100顶部引出以氮气为主要成分的气体物流4，依次返回E-102、E-101和E-100中，温度复温到常温，为换热器提供冷量；气提塔T-100塔底部物流11经J-T阀节流得到高纯度的液态天然气。气液分离罐V-100分离出的气体物流2依次返回E-101和E-100中，物流3复温到常温。
低压氮气物流7经过压缩机C-100和冷却器E-104压缩、冷却到常温，物流8进入透平膨胀机EXP-100的增压机C-101中继续压缩，经过冷却器E-105冷却到常温后的物流9依次经过换热器E-100和E-101中冷却，物流10的温度达到-110℃左右的氮气进入透平膨胀机EXP-100中进行膨胀制冷，膨胀后的物流11的温度达到-160℃左右，依次进入换热器E-101和E-100，为换热器提供冷量。
本发明中的换热器E-100和E-101也可以合并为一台换热器，工程中根据实际需要的换热面积，选择合适的换热器个数。
此外，图1、图2和图3所示的流程示意图并不是固定模式，根据实际情况，对混合制冷剂制冷系统的压缩和分离级数、节流级数进行调整，重烃分离罐也可以取消，氮气制冷系统可以选择单路膨胀和双路膨胀，冷箱内的换热器数量可以根据换热器的类型和厂家的制造能力增加和较少换热器数量。对于气液分离器分离出的富氢气的气体，气提塔塔底的富氮气的气体，根据配套的处理设施可以分别复温或汇合一起后进行复温。

Claims (9)

1.一种焦炉煤气制取液化天然气的方法，包括如下步骤：
（1）将焦炉煤气原料气进行压缩冷却；
（2）将经冷却后的焦炉煤气分成两股：焦炉煤气物流A和焦炉煤气物流B；所述焦炉煤气物流B经J-T阀节流降压和冷却后进入至气提塔塔底；
（3）所述焦炉煤气物流A经冷却后进入至气液分离罐中；所述气液分离罐的底部出来的液体物流进入气提塔；所述气提塔塔底的物流经J-T阀节流即得液化天然气；
所述冷却均在换热器中进行。
2.根据权利要求1所述的方法，其特征在于：所述气液分离罐底部的物流从所述气提塔的顶部进入至所述气提塔中。
3.根据权利要求1或2所述的方法，其特征在于：所述焦炉煤气原料气经压缩冷却后进入重烃分离罐。
4.根据权利要求1-3中任一所述的方法，其特征在于：步骤（2）中，将所述焦炉煤气物流B冷却至-120℃~-150℃；所述冷却过程为所述气提塔提供热量。
5.根据权利要求1-4中任一所述的方法，其特征在于：步骤（3）中，将所述焦炉煤气物流A冷却至-140℃～-160℃。
6.根据权利要求1-5中任一所述的方法，其特征在于：所述换热器组的冷量由制冷系统提供；所述制冷系统为混合冷剂制冷系统或气体膨胀制冷系统。
7.根据权利要求1-6中任一所述的方法，其特征在于：从所述气液分离罐的顶部出来的物流经所述换热器复温。
8.根据权利要求1-7中任一所述的方法，其特征在于：从所述气提塔塔顶出来的物流经所述换热器复温。
9.根据权利要求1-8中任一所述的方法，其特征在于：所述换热器为板翅换热器或绕管式换热器。
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CN104031710A (zh) * 2014-06-27 2014-09-10 中国海洋石油总公司 一种利用焦炉气生产液化天然气的工艺
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CN113355135A (zh) * 2021-03-19 2021-09-07 北京欧谊德科技有限公司 一种炼厂饱和干气的分离方法
CN113350974A (zh) * 2021-03-19 2021-09-07 北京欧谊德科技有限公司 一种饱和干气中h2、c1、c2和c3的分离回收方法

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