CN104628505B - 一种从液化天然气中回收乙烷的方法及装置 - Google Patents

一种从液化天然气中回收乙烷的方法及装置 Download PDF

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CN104628505B
CN104628505B CN201310573794.6A CN201310573794A CN104628505B CN 104628505 B CN104628505 B CN 104628505B CN 201310573794 A CN201310573794 A CN 201310573794A CN 104628505 B CN104628505 B CN 104628505B
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王勇
夏政
林罡
郭亚红
张丽娟
张玉玺
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Abstract

一种从液化天然气中回收乙烷的方法及装置，属于LNG（液化天然气）回收乙烷工艺技术领域。LNG泵连接第一分配器，第一分配器连接板翅式换热器、脱甲烷塔，脱甲烷塔连接回流泵、脱乙烷塔，翅式换热器连接回流罐、第一循环器、脱甲烷塔、脱乙烷塔，第一循环器连接脱甲烷塔，回流罐连接回流泵，回流泵连接第二分配器；第二分配器连接第二循环器；第二循环器连接脱乙烷塔，乙烷塔连接平衡器。本发明结构简单，通过板翅式换热器各物流间的换热来提供该装置的质量平衡和能量平衡。通过脱甲烷塔实现LNG中甲烷的分离；通过脱乙烷塔可实现LNG中乙烷的分离。最终所回收的乙烷纯度可达到94%；出来的液化气也满足我国液化气的标准。

Description

一种从液化天然气中回收乙烷的方法及装置
技术领域
本发明涉及一种从液化天然气中回收乙烷的方法及装置，属于LNG（液化天然气）回收乙烷工艺技术领域。
背景技术
随着我国石化市场持续迅猛的发展，对石化基础原料的要求也越来越高，原料来源成为制约乙烯产业发展的关键。目前，我国乙烯原料主要来自石脑油，而石脑油全部来自石油，近年来石油价格居高不下，不但提高了乙烯生产成本，而且原料成本也占乙烯生产成本的60%～80%，压缩了乙烯的利润空间。因此，寻找乙烯原料就十分必要。
发明内容
为了克服现有技术的不足,本发明提供一种从液化天然气中回收乙烷的方法及装置。
本发明的目的是采用LNG作为原料回收乙烷，即提供一种回收乙烷的方法。从LNG中回收乙烷、丙烷、丁烷作为乙烯原料，不但乙烯收率高，而且可以节省大量宝贵和紧缺的燃料油，并能有效缓解市场油品的供需矛盾。
一种从液化天然气中回收乙烷的装置,LNG泵连接第一分配器，第一分配器连接板翅式换热器、脱甲烷塔，脱甲烷塔连接回流泵、脱乙烷塔，翅式换热器连接回流罐、第一循环器、脱甲烷塔、脱乙烷塔，第一循环器连接脱甲烷塔，回流罐连接回流泵，回流泵连接第二分配器；第二分配器连接第二循环器；第二循环器连接脱乙烷塔，乙烷塔连接平衡器。
平衡器输出液化气；LNG进入LNG泵；第二分配器输出乙烷；翅式换热器输出甲烷。
一种从液化天然气中回收乙烷的方法,至少包括LNG泵、分配器、脱甲烷塔、脱乙烷塔、冷箱、回流罐、回流泵组成；将LNG增压后，一部分作为冷剂，另一部分进入脱甲烷塔，经过精馏后脱出介质甲烷，塔底液体进入脱乙烷塔，经过精馏后，塔顶乙烷合格后作为产品外输，塔底液体为液化气。
含有以下步骤；
LNG（温度-162℃，压力0.12MPa）经过LNG泵增压后，增压至4.5MPa，再经第一分配器分成两股物流，其中第二物流占总流量的61%；第三物流占总流量的39%；第二物流通过管道进入脱甲烷塔6的顶部；将脱甲烷塔的压力控制在3.6～3.62MPa，以保证大部分甲烷脱出，脱甲烷塔塔底甲烷含量控制在1%左右；重沸器温度控制在50.6℃，并在此温度下精馏，脱甲烷塔塔底出来的第六物流（温度50.6℃，压力3.62MPa），通过管道继续输送到脱乙烷塔；脱乙烷塔压力控制在2.97～3.0MPa，为保证大部分乙烷脱出，脱乙烷塔塔底乙烷含量控制在1%左右；脱乙烷塔塔内重沸器温度设定在92.1℃，在此温度下塔内进行二次精馏，脱乙烷塔塔底出来的液化气（温度92.11℃,压力3.0MPa）经过平衡器测试：37.8℃下脱乙烷塔液化气的饱和蒸气压为1023kPa，满足GB11174-89中所规定的炼厂液化石油气在37.8℃下的蒸汽压不大于1380kPa；脱乙烷塔塔顶出来的第七物流（温度12.56℃，压力2.97MPa）乙烷含量达到94%，回收效果良好；
从第一分配器分出来的另一股LNG第三物流（温度-159.9℃，压力4.5MPa），经过板翅式换热器被加热，第十四物流（温度-55℃，压力4.49MPa）进入第一循环器循环，第十四物流进入脱甲烷塔；
脱甲烷塔塔顶出来的甲烷第五物（温度-84.36℃，压力3.6MPa），甲烷含量为0.99%，基本满足所控制的要求；再经过板翅式换热器被加热，物流甲烷（温度7.4℃，压力3.59MPa）输送到下游作为燃料气外输；
脱乙烷塔出来的乙烷，第七物流（温度12.6℃，压力2.97MPa）经过板翅式换热器被冷却，第八物（温度-18℃，压力2.96MPa）进入回流罐，经回流罐罐中缓冲分离后，第十物流经回流泵增压至3.2MPa，进入第二分配器进行二次分配；分配后一部分乙烷进入第二循环器打循环，重新打入到脱乙烷塔进行二次精馏，建立此循环的目的是通过不断让含有其它成分的乙烷不断进入脱乙烷塔进行反复精馏，最终提高乙烷纯度；另一部分乙烷作为产品外输，模拟计算中纯度可达到94%左右。
本发明结构简单，通过分析LNG中的各组分，提出了一种从LNG中回收乙烷的工艺方法及工艺装置。该方法可通过利用LNG本身的低温，并通过板翅式换热器各物流间的换热来提供该装置的质量平衡和能量平衡。通过脱甲烷塔实现LNG中甲烷的分离；通过脱乙烷塔可实现LNG中乙烷的分离。最终所回收的乙烷纯度可达到94%；出来的液化气也满足我国液化气的标准。该装置可适用于各地区的LNG调峰站，生产出的甲烷和液化气可满足下游用户的日常用气要求，生产出的乙烷可满足国民经济生产中对乙烯的需求。同时所有设备、管道及阀门工艺管线可实现橇装化安装、数字化管理、实时远程控制；另外，脱甲烷塔所需热负荷为50℃左右、脱乙烷塔所需热负荷为90℃左右，可就近采用锅炉蒸汽或者导热油加热，易方便操作。
附图说明
当结合附图考虑时，通过参照下面的详细描述，能够更完整更好地理解本发明以及容易得知其中许多伴随的优点，但此处所说明的附图用来提供对本发明的进一步理解，构成本发明的一部分，本发明的示意性实施例及其说明用于解释本发明，并不构成对本发明的不当限定，其中：
图1为本发明的实施结构示意图。
下面结合附图和实施例对本发明进一步说明。
具体实施方式
显然，本领域技术人员基于本发明的宗旨所做的许多修改和变化属于本发明的保护范围。
实施例1：如图1所示，一种用LNG回收乙烷的装置，LNG泵2连接第一分配器3，第一分配器3连接板翅式换热器4、脱甲烷塔6，脱甲烷塔6连接回流泵13、脱乙烷塔7，翅式换热器4连接回流罐14、第一循环器5、脱甲烷塔6、脱乙烷塔7，第一循环器5连接脱甲烷塔6，回流罐14连接回流泵13，回流泵13连接第二分配器12；第二分配器12连接第二循环器10；第二循环器10连接脱乙烷塔7，乙烷塔7连接平衡器8。
平衡器8输出液化气9；LNG1进入LNG泵2；第二分配器12输出乙烷11；翅式换热器4输出甲烷15。
实施例2：如图1所示，一种从液化天然气中回收乙烷的方法,含有以下步骤；
至少包括LNG泵、分配器、脱甲烷塔、脱乙烷塔、冷箱、回流罐、回流泵组成；将LNG增压后，一部分作为冷剂，另一部分进入脱甲烷塔，经过精馏后脱出介质甲烷，塔底液体进入脱乙烷塔，经过精馏后，塔顶乙烷合格后作为产品外输，塔底液体为液化气，符合我国炼厂液化石油气的质量指标。
经第一分配器3分成两股物流，其中第二物流22占总流量的61%；第三物流23占总流量的39%；第二物流22通过管道进入脱甲烷塔6的顶部；将脱甲烷塔6的压力控制在3.6～3.62MPa，以保证大部分甲烷脱出，脱甲烷塔6塔底甲烷含量控制在1%左右；重沸器温度控制在50.6℃，并在此温度下精馏，脱甲烷塔6塔底出来的第六物流26（温度50.6℃，压力3.62MPa），通过管道继续输送到脱乙烷塔7；脱乙烷塔7压力控制在2.97～3.0MPa，为保证大部分乙烷脱出，脱乙烷塔7塔底乙烷含量控制在1%左右；脱乙烷塔7塔内重沸器温度设定在92.1℃，在此温度下塔内进行二次精馏，脱乙烷塔7塔底出来的液化气（温度92.11℃,压力3.0MPa）经过平衡器测试：37.8℃下脱乙烷塔液化气的饱和蒸气压为1023kPa，满足GB11174-89中所规定的炼厂液化石油气在37.8℃下的蒸汽压不大于1380kPa；脱乙烷塔7塔顶出来的第七物流27（温度12.56℃，压力2.97MPa）乙烷含量达到94%，回收效果良好；
从第一分配器3分出来的另一股LNG第三物流23（温度-159.9℃，压力4.5MPa），经过板翅式换热器被加热，第十四物流24（温度-55℃，压力4.49MPa）进入第一循环器5循环，第十四物流34进入脱甲烷塔6；
脱甲烷塔6塔顶出来的甲烷第五物流25（温度-84.36℃，压力3.6MPa），甲烷含量为0.99%，基本满足所控制的要求；再经过板翅式换热器4被加热，物流甲烷（温度7.4℃，压力3.59MPa）输送到下游作为燃料气外输；
脱乙烷塔7出来的乙烷，第七物流27（温度12.6℃，压力2.97MPa）经过板翅式换热器4被冷却，第八物流28（温度-18℃，压力2.96MPa）进入回流罐14，经回流罐14罐中缓冲分离后，第十物流30经回流泵13增压至3.2MPa，进入第二分配器12进行二次分配；分配后一部分乙烷进入第二循环器10打循环，重新打入到脱乙烷塔7进行二次精馏，建立此循环的目的是通过不断让含有其它成分的乙烷不断进入脱乙烷塔7进行反复精馏，最终提高乙烷纯度；另一部分乙烷作为产品外输，模拟计算中纯度可达到94%左右。
表-1为LNG组成表。
表-1
如上所述，对本发明的实施例进行了详细地说明，但是只要实质上没有脱离本发明的发明点及效果可以有很多的变形，这对本领域的技术人员来说是显而易见的。因此，这样的变形例也全部包含在本发明的保护范围之内。

Claims (3)

1.一种从液化天然气中回收乙烷的装置，其特征在于LNG泵连接第一分配器，第一分配器连接板翅式换热器、脱甲烷塔，脱甲烷塔连接回流泵、脱乙烷塔，翅式换热器连接回流罐、第一循环器、脱甲烷塔、脱乙烷塔，第一循环器连接脱甲烷塔，回流罐连接回流泵，回流泵连接第二分配器；第二分配器连接第二循环器；第二循环器连接脱乙烷塔，乙烷塔连接平衡器。
2.一种从液化天然气中回收乙烷的方法,至少包括LNG泵、分配器、脱甲烷塔、脱乙烷塔、冷箱、回流罐、回流泵组成；将LNG增压后，一部分作为冷剂，另一部分进入脱甲烷塔，经过精馏后脱出介质甲烷，塔底液体进入脱乙烷塔，经过精馏后，塔顶乙烷合格后作为产品外输，塔底液体为液化气。
3.根据权利要求2所述的一种从液化天然气中回收乙烷的方法，其特征在于含有以下步骤；
温度为-162℃且压力为0.12MPa的LNG经过LNG泵增压后，增压至4.5MPa，再经第一分配器分成两股物流，其中第二物流占总流量的61％；第三物流占总流量的39％；第二物流通过管道进入脱甲烷塔6的顶部；将脱甲烷塔的压力控制在3.6～3.62MPa，以保证大部分甲烷脱出，脱甲烷塔塔底甲烷含量控制在1％左右；重沸器温度控制在50.6℃，并在此温度下精馏，脱甲烷塔塔底出来的温度为50.6℃且压力为3.62MPa第六物流，通过管道继续输送到脱乙烷塔；脱乙烷塔压力控制在2.97～3.0MPa，为保证大部分乙烷脱出，脱乙烷塔塔底乙烷含量控制在1％左右；脱乙烷塔塔内重沸器温度设定在92.1℃，在此温度下塔内进行二次精馏，脱乙烷塔塔底出来的温度为92.11℃且压力为3.0MPa液化气经过平衡器测试：37.8℃下脱乙烷塔液化气的饱和蒸气压为1023kPa，满足GB11174-89中所规定的炼厂液化石油气在37.8℃下的蒸汽压不大于1380kPa；脱乙烷塔塔顶出来的温度为12.56℃且压力为2.97MPa的第七物流乙烷含量达到94％；
从第一分配器分出来的温度为-159.9℃且压力为4.5MPa的另一股LNG第三物流，经过板翅式换热器被加热，温度为-55℃且压力为4.49MPa的第十四物流进入第一循环器循环，第十四物流进入脱甲烷塔；
脱甲烷塔塔顶出来的温度为-84.36℃且压力为3.6MPa的甲烷第五物，甲烷含量为0.99％，基本满足所控制的要求；再经过板翅式换热器被加热，温度为7.4℃且压力为3.59MPa的物流甲烷输送到下游作为燃料气外输；
脱乙烷塔出来的乙烷，温度为12.6℃且压力为2.97MPa的第七物流经过板翅式换热器被冷却，温度为-18℃且压力为2.96MPa的第八物进入回流罐，经回流罐罐中缓冲分离后，第十物流经回流泵增压至3.2MPa，进入第二分配器进行二次分配；分配后一部分乙烷进入第二循环器打循环，重新打入到脱乙烷塔进行二次精馏；另一部分乙烷作为产品外输。
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