CN102654348B - 一种焦炉煤气制取液化天然气的方法 - Google Patents

一种焦炉煤气制取液化天然气的方法 Download PDF

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CN102654348B
CN102654348B CN201210159925.1A CN201210159925A CN102654348B CN 102654348 B CN102654348 B CN 102654348B CN 201210159925 A CN201210159925 A CN 201210159925A CN 102654348 B CN102654348 B CN 102654348B
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coke
coke oven
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CN102654348A (zh
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唐令力
单彤文
陈杰
王秀林
尹全森
花亦怀
曾伟平
刘淼儿
李恩道
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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经冷却后与所述焦炉煤气物流A混合后进入换热器组进行热量交换；（3）从所述换热器组出来的焦炉煤气出来后进入至气液分离罐；（4）所述气液分离罐的底部出来的物流进入精馏塔；所述精馏塔塔底的物流进入至设置于所述精馏塔塔底的再沸器；从所述再沸器中出来的物流再经J-T阀节流即得。本发明结合我国焦炉煤气利用的现状提出采用低温精馏的方法，将甲烷从焦炉煤气中分离出来，制成液化天然气，整套工艺具有流程简单、操作方便、甲烷回收率和LNG产品的纯度高、总体能耗低的优点。

Description

一种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
本发明的目的是提供一种焦炉煤气制取液化天然气的方法，本方法制取的液化天然气纯度可达到99%以上，整套工艺简单、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经冷却后与所述焦炉煤气物流A混合后进入换热器组进行热量交换；
（3）从所述换热器组出来的焦炉煤气出来后进入至气液分离罐；
（4）所述气液分离罐的底部出来的物流进入精馏塔；所述精馏塔的塔底物流进入至设置于所述精馏塔塔底的再沸器；从所述再沸器中出来的物流再经J-T阀节流即得液化天然气。
上述的方法中，所述气液分离罐底部的物流从所述精馏塔的中部进入至所述精馏塔中。
上述的方法中，从所述再沸器中出来的物流经冷却后再经所述J-T阀节流得到液化天然气。
上述的方法中，将从所述再沸器中出来的物流冷却至-150℃～-162℃，如-160℃。
上述的方法中，所述换热器组的冷量由制冷***提供；所述制冷***可为气体膨胀制冷***或混合冷剂制冷***。
上述的方法中，步骤（2）中，将所述焦炉煤气物流B冷却至-20℃～-120℃，如-120℃，所述冷却过程为所述再沸器提供热量。
上述的方法中，所述焦炉煤气物流A和焦炉煤气物流B混合后经所述换热器组冷却至-140℃～-160℃，如-155℃。
上述的方法中，从所述气液分离罐的顶部出来的物流经所述换热器组复温。
上述的方法中，从所述精馏塔塔顶出来的物流经所述换热器组复温。
本发明结合我国焦炉煤气利用的现状提出采用低温精馏的方法，将甲烷从焦炉煤气中分离出来，制成液化天然气，整套工艺具有流程简单、操作方便、甲烷回收率和LNG产品的纯度高、总体能耗低的优点。
附图说明
图1和图2均为本发明实施例1中混合冷剂制冷循环制取LNG的流程示意图；
图3为本发明实施例2中气体膨胀制冷循环制取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、
本实施例为采用混合工质制冷、精馏法制取LNG的一种流程示意图。
如图1所示，该工艺流程主要包括制冷***、换热设备和分离设备；其中制冷设备为气体压缩机和J-T阀，换热设备包括冷箱和空冷/水冷换热器，分离设备包括气液分离罐和精馏塔；精馏塔设置有再沸器和冷凝器，进一步提高LNG的纯度和增加甲烷回收率；该套工艺还包括混合冷剂压缩机和冷凝器。
其工艺流程如下：
如图1所示：将含H2、N2的焦炉煤气经冷却器E-100冷却后分成两股物流A和B，焦炉煤气物流B经再沸器E-102冷却至-120℃左右，为精馏塔T-100底部再沸器提供热源后，与焦炉煤物流A混合，经换热器E-101冷却至-155℃后，进入气液分离罐V-100，经气液分离罐V-100分离出大部分H2后的液相物流1，从中部进入精馏塔T-100，在精馏塔T-100内物流经过充分的质、热交换后，精馏塔T-100顶部引出以氮气和氢气为主的驰放气，精馏塔T-100塔底部物流15经J-T阀节流得到高纯度的液态天然气；从气液分离罐V-100分离出的气体物流2先后进入进入换热器E-101和E-100，为这两换热器提供部分冷源，物流3的温度复温到常温。精馏塔T-100顶部引出的气体物流4进入精馏塔的冷凝器E-103，物流4中的甲烷在E-103冷凝后，进入气液分离器V-102，液体物流5返回精馏塔，作为精馏塔的回流液；在V-102中分离的气体物流6以氮气和氢气为主，依次进入E-101和E-100，温度复温到常温。混合冷剂工质物流7经过压缩机C-100压缩和冷却器E-104冷却后，进入气液分离器V-101分离出液体物流8和气相物流9，气相物流经过压缩机C-101压缩，液体物流经过液体泵P-100加压，两股液体汇合后进入冷却器E-105中冷却到常温，常温和高压的两相混合制冷工质物流10依次进入换热器E-100和E-101，从E-101中出来的物流11的温度达到-155℃，分成两股物流12和物流13，物流12节流制冷后为精馏塔的冷凝器E-103提供冷源，从E-103中出来的物流14与物流13节流后物流汇合，依次进入E-101和E-100，为焦炉气冷却和冷凝提供冷源。
如图2所示：将含H2、N2的焦炉煤气经冷却器E-100冷却后分成两股物流A和B，焦炉煤气物流B经再沸器E-102冷却至-120℃左右，为精馏塔T-100底部再沸器提供热源后，与焦炉煤物流A混合，经换热器E-101冷却至-150℃后，进入气液分离罐V-100，经气液分离罐V-100分离出大部分H2后的液相物流1，从中部进入精馏塔T-100，在精馏塔T-100内物流经过充分的质、热交换后，精馏塔T-100顶部引出以氮气和氢气为主的驰放气，精馏塔T-100塔底部物流16进入换热器E-106中冷却，冷却到-160℃左右，再经J-T阀节流得到高纯度的液态天然气，增加液化天然气过冷后，减少节流后的闪蒸气体量，闪蒸气体处理***减少；从气液分离罐V-100分离出的气体物流2进入先后进入换热器E-101和E-100，为这两换热器提供部分冷源，物流3的温度复温到常温。精馏塔T-100顶部引起的气体物流4进入精馏塔的冷凝器E-103，物流4中的甲烷在E-103冷凝后，进入气液分离器V-102，液体物流5返回精馏塔，作为精馏塔的回流液；在V-102中分离的气体物流6以氮气和氢气为主，依次进入E-101和E-100，温度复温到常温。混合冷剂工质物流7经过压缩机C-100压缩和冷却器E-104冷却后，进入气液分离器V-101分离出液体物流8和气相物流9，气相物流经过压缩机C-101压缩，液体物流经过液体泵P-100加压，两股液体汇合后进入冷却器E-105中冷却到常温，常温和高压的两相混合制冷工质物流10依次进入换热器E-100和E-101，从E-101中出来的物流11的温度达到-160℃，分成两股物流12和物流13，物流12节流制冷后为精馏塔的冷凝器E-103提供冷源，物流13节流制冷后为换热器E-106提供冷量，从E-103和E-106中出来的物流14与物流15汇合，依次进入E-101和E-100，为焦炉气冷却和冷凝提供冷源。
实施例2、
本实施例为采用氮膨胀制冷、精馏法制取LNG的一种流程示意图。
如图3所示，该工艺流程主要包括制冷***、换热设备和分离设备；其中制冷设备为气体压缩机和膨胀机，换热设备包括冷箱和空冷/水冷换热器，分离设备包括气液分离罐罐和精馏塔；精馏塔设置有再沸器和冷凝器，进一步提高LNG的纯度和甲烷的回收率。该套工艺还包括N2压缩机和冷凝器，氮膨胀制冷***为整套工艺提供冷源。
具体流程为：将含H2、N2的焦炉煤气经冷却器E-100冷却后分成两股物流A和B，焦炉煤气物流B经再沸器E-102冷却至-120℃左右，为精馏塔T-100底部再沸器提供热源后，与焦炉煤物流A混合，经换热器E-101冷却至-155℃后，进入气液分离罐V-100，经气液分离罐V-100分离出大部分H2后的液相物流1，从中部进入精馏塔T-100，在精馏塔T-100内物流经过充分的质、热交换后，精馏塔T-100顶部引出以氮气和氢气为主的驰放气，精馏塔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；从气液分离罐V-100分离出的气体物流2进入先后进入换热器E-101和E-100，为这两换热器提供部分冷源，物流3的温度复温到常温。精馏塔T-100顶部引出的气体物流4进入精馏塔的冷凝器E-103，物流4中的甲烷在E-103冷凝后，进入气液分离器V-102，液体物流5返回精馏塔，作为精馏塔的回流液；在V-101中分离的气体物流6以氮气和氢气为主，依次进入E-101和E-100，温度复温到常温。氮气物流7经过压缩机C-100压缩和冷却器E-104冷却后，进入透平膨胀机EXP-100的增压机C-101中继续压缩后，进入冷却器E-105中冷却到常温后的物流9依次进入换热器E-100和E-101，从E-101中出来的物流10的温度达到-120℃左右，进入透平膨胀机EXP-100中膨胀制冷，物流11的温度达到-170℃左右，为精馏塔的冷凝器E-103提供冷源，从E-103中出来的物流12再依次进入E-101和E-100，为焦炉气冷却和冷凝提供冷源。

Claims (2)

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经冷却后与所述焦炉煤气物流A混合后进入换热器组进行热量交换；
所述换热器组的冷量由一套制冷***提供；所述制冷***为气体膨胀制冷***或混合冷剂制冷***；
（3）从所述换热器组出来的焦炉煤气出来后进入至气液分离罐；
（4）所述气液分离罐的底部出来的物流进入精馏塔；所述精馏塔塔底的物流进入至设置于所述精馏塔塔底的再沸器；从所述再沸器中出来的物流再经J-T阀节流，即得液化天然气；
从所述气液分离罐的顶部出来的物流经所述换热器组复温；
从所述精馏塔塔顶出来的物流经所述换热器组复温；
所述气液分离罐底部的物流从所述精馏塔的中部进入至所述精馏塔中；
从所述再沸器中出来的物流经冷却后再经J-T阀节流得到液化天然气；
步骤（2）中，将所述焦炉煤气物流B冷却至-20℃~-120℃，所述冷却过程为所述再沸器提供热量；
所述焦炉煤气物流A和焦炉煤气物流B混合后经所述换热器组冷却至-140℃~-160℃。
2.根据权利要求1所述的方法，其特征在于：将从所述再沸器中出来的物流冷却至-150℃~-162℃。
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