CN109210867A - 一种从含氧煤层气中回收甲烷的系统 - Google Patents

一种从含氧煤层气中回收甲烷的系统 Download PDF

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CN109210867A
CN109210867A CN201810990064.9A CN201810990064A CN109210867A CN 109210867 A CN109210867 A CN 109210867A CN 201810990064 A CN201810990064 A CN 201810990064A CN 109210867 A CN109210867 A CN 109210867A
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孙守军
公茂琼
郭浩
孙恒
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Technical Institute of Physics and Chemistry of CAS
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Abstract

本发明提供的从含氧煤层气中回收甲烷的系统包括：制冷模块、深冷分离储存模块、尾气燃烧模块，所述制冷模块包括吸收式制冷预冷单元以及混合制冷剂制冷液化单元，本发明提供的从含氧煤层气中回收甲烷的系统采用单一混合制冷剂液化循环组成的液化循环，以及低温精馏组成的深冷分离过程，可以在不脱除氧气的前提下，保证整个甲烷回收过程的安全，并能够充分利用尾气中的甲烷资源来降低整个系统的能耗，实现节能。

Description

一种从含氧煤层气中回收甲烷的系统
技术领域
本发明涉及含氧煤层气利用领域，尤其涉及一种从含氧煤层气中回收甲烷的系统。
背景技术
我国煤层气资源丰富，合理利用煤层气在抽采过程中形成的含氧煤层气，不仅能够提高煤层气利用率，提升煤矿开采的安全性，并且能够减少煤层气的排放量，减少对于大气环境的污染。含氧煤层气中主要利用的组分为甲烷，甲烷是重要的能源燃料以及化工原料。但是含氧煤层气中由于含氧的缘故，使得在其甲烷回收的过程中需要考虑由于含氧带来的安全问题。
随着科学技术的不断发展，陆续产生了多中含氧煤层气液化分离流程，而现有的技术专利主要分为两类，一类是直接脱氧后再进行含氧煤层气中的甲烷和氮气的分离，一类是没有进行脱氧，但是追求含氧煤层气中甲烷的完全的回收，而没有考虑由于含氧给带甲烷回收过程带来的安全问题。
发明内容
有鉴如此，有必要针对现有技术存在的缺陷，提供一种可保证甲烷回收过程安全的的回收甲烷系统。
为实现上述目的，本发明采用下述技术方案：
一种从含氧煤层气中回收甲烷的系统，包括：制冷模块、深冷分离储存模块、尾气燃烧模块；其中：
所述制冷模块包括吸收式制冷预冷单元以及混合制冷剂制冷液化单元；
所述吸收式制冷预冷单元包括塔底重沸器、制冷精馏塔、塔顶冷凝器、一次分离器、冷凝器、吸收式制冷预冷换热器、吸收式制冷预冷节流阀、回热冷凝器、制冷剂溶液泵、吸收式制冷回热换热器及吸收式制冷回热节流阀，所述制冷精馏塔、塔顶冷凝器、一次分离器、冷凝器、预冷换热器及吸收式制冷节流阀通过管道依次连接，所述吸收式制冷节流阀通过管道依次经所述吸收式制冷预冷换热器、回热冷凝器、制冷剂溶液泵及吸收式制冷回热换热器连接所述制冷精馏塔，所述塔底重沸器连接于所述制冷精馏塔的下方，且所述塔底重沸器的一端通过管道依次经所述连接吸收式制冷回热换热器、所述吸收式制冷回热节流阀连接所述制冷精馏塔；
所述混合冷剂制冷液化单元包括由混合冷剂压缩机及混合冷剂冷凝器组成的压缩机组件、混合冷剂节流阀、煤层气预冷换热器、煤层气一级液化换热器、煤层气二级液化换热器、煤层气三级液化换热器，所述混合冷剂压缩机入口连接所述煤层气一级液化换热器的制冷剂出口，所述混合冷剂压缩机出口连接所述混合冷剂冷凝器入口，所述混合冷剂冷凝器出口依次连接所述煤层气预冷换热器、所述煤层气一级液化换热器及所述煤层气二级液化换热器，所述煤层气二级液化换热器的制冷剂出口与所述塔底重沸器制冷剂入口相连，所述塔底重沸器制冷剂出口与所述煤层气三级液化换热器制冷剂入口相连，所述煤层气三级液化换热器制冷剂出口与所述混合冷剂节流阀入口相连，所述混合冷剂节流阀出口与塔顶冷凝器相连，所述塔顶冷凝器制冷剂出口依次与所述煤层气三级液化换热器、所述煤层气二级液化换热器、所述煤层气一级液化换热器相连，实现循环；
所述深冷分离储存模块包括深冷节流阀、深冷分离精馏塔、深冷分离精馏塔塔顶冷凝器、深冷分离精馏塔塔顶分离器、深冷分离精馏塔重沸器及LNG储罐，所述深冷节流阀的入口与所述煤层气三级液化换热器、煤层气二级液化换热器、煤层气一级液化换热器及煤层气预冷换热器分别连接，所述深冷节流阀的出口与所述深冷分离精馏塔入口相连，所述深冷分离精馏塔的塔底与所述LNG储罐相连接，所述深冷分离精馏塔塔顶冷凝器的出口与所述深冷分离精馏塔塔顶分离器相连，所述深冷分离精馏塔塔顶分离器的气相出口依次与所述煤层气三级液化换热器、所述煤层气二级液化换热器、所述煤层气一级液化换热器及所述煤层气预冷换热器连接后与所述尾气燃烧模块相连接；
所述尾气燃烧模块包括尾气燃烧器，所述尾气燃烧器包含空气入口和尾气入口，所述尾气燃烧器燃烧产物出口与所述塔底重沸器相连。
在一些较佳的实施例中，所述吸收式制冷预冷单元包括的吸收式制冷剂为氨-水制冷剂。
在一些较佳的实施例中，所述混合制冷剂制冷液化单元包括的混合制冷剂为天然制冷剂，所述天然制冷剂为由氮气、甲烷、乙烷、丙烷、异丁烷和戊丁烷以任意配比组成的混合物。
在一些较佳的实施例中，所述压缩机组件包括至少一对所述混合冷剂压缩机及混合冷剂冷凝器的组合。
在一些较佳的实施例中，所述压缩机组件中包括三对所述混合冷剂压缩机及混合冷剂冷凝器的组合。
在一些较佳的实施例中，经所述精馏塔塔顶尾气中甲烷含量高于爆炸上限接。
在一些较佳的实施例中，所述含氧煤层气由甲烷、氮气及氧气组成。
本发明采用上述技术方案的优点是：
本发明提供的从含氧煤层气中回收甲烷的系统，可以在不脱除氧气的前提下，保证整个甲烷回收过程的安全，并能够充分利用尾气中的甲烷资源来降低整个系统的能耗，实现节能。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其它的附图。
图1为本发明实施例提供的从含氧煤层气中回收甲烷的系统的结构示意图。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其它实施例，都属于本发明保护的范围。
请参阅图1，为本发明实施例提供的从含氧煤层气中回收甲烷的系统10的结构示意图，包括：制冷模块、深冷分离储存模块120、尾气燃烧模块130。以下详细说明各个部件的具体结构。
所述制冷模块包括吸收式制冷预冷单元111以及混合制冷剂制冷液化单元112。其中：
所述吸收式制冷预冷单元111包括塔底重沸器15、制冷精馏塔16、塔顶冷凝器17、一次分离器18、冷凝器19、吸收式制冷预冷换热器20、吸收式制冷预冷节流阀21、回热冷凝器22、制冷剂溶液泵23、吸收式制冷回热换热器24及吸收式制冷回热节流阀25。所述吸收式制冷预冷单元111各个部件连接如下：所述制冷精馏塔16、塔顶冷凝器17、一次分离器18、冷凝器19、吸收式制冷预冷换热器20及吸收式制冷节流阀21通过管道依次连接，所述吸收式制冷节流阀21通过管道依次经所述吸收式制冷预冷换热器20、回热冷凝器22、制冷剂溶液泵23及吸收式制冷回热换热器24连接所述制冷精馏塔16，所述塔底重沸器15连接于所述制冷精馏塔16的下方，且所述塔底重沸器15的一端通过管道依次经所述连接吸收式制冷回热换热器24、所述吸收式制冷回热节流阀25连接所述制冷精馏塔16。
在一些较佳的实施例中，所述吸收式制冷预冷单元111包括的吸收式制冷剂为氨-水制冷剂。
所述混合冷剂制冷液化单元112包括由混合冷剂压缩机11及混合冷剂冷凝器12组成的压缩机组件、混合冷剂节流阀13、煤层气预冷换热器1、煤层气一级液化换热器2、煤层气二级液化换热器3、煤层气三级液化换热器4，所述混合冷剂压缩机11入口连接所述煤层气一级液化换热器2的制冷剂出口，所述混合冷剂压缩机11出口连接所述混合冷剂冷凝器12的入口，所述混合冷剂冷凝器12的出口依次连接所述煤层气预冷换热器1、所述煤层气一级液化换热器2及所述煤层气二级液化换热器3，所述煤层气二级液化换热器2的制冷剂出口与所述塔底重沸器15制冷剂入口相连，所述塔底重沸器15制冷剂出口与所述煤层气三级液化换热器4制冷剂入口相连，所述煤层气三级液化换热器4的制冷剂出口与所述混合冷剂节流阀13的入口相连，所述混合冷剂节流阀13的出口与塔顶冷凝器17相连，所述塔顶冷凝器17的制冷剂出口依次与所述煤层气三级液化换热器4、所述煤层气二级液化换热器3、所述煤层气一级液化换热器2相连，实现循环。
在一些较佳的实施例中，所述混合制冷剂制冷液化单元112包括的混合制冷剂为天然制冷剂，所述天然制冷剂为由氮气、甲烷、乙烷、丙烷、异丁烷和戊丁烷以任意配比组成的混合物。
在一些较佳的实施例中，所述压缩机组件包括至少一对所述混合冷剂压缩机11及混合冷剂冷凝器12的组合。可以理解，可以根据实际生产需要设置多对混合冷剂压缩机和混合冷剂冷凝器组合，且优选为所述压缩机组件中包括三对所述混合冷剂压缩机及混合冷剂冷凝器的组合。
可以理解，在所述吸收式制冷预冷单元111中，流经吸收式制冷回热节流阀25、吸收式制冷预冷换热器20以及煤层气预冷换热器1的制冷剂依次通过回热冷凝器22、制冷剂溶液泵23、吸收式制冷回热换热器24连通于制冷精馏塔16实现循环。
所述深冷分离储存模块120包括深冷节流阀5、深冷分离精馏塔6、深冷分离精馏塔塔顶冷凝器8、深冷分离精馏塔塔顶分离器9、深冷分离精馏塔重沸器7及LNG储罐10，所述深冷节流阀5的入口与所述煤层气三级液化换热器4、煤层气二级液化换热器3、煤层气一级液化换热器2及煤层气预冷换热器1分别连接，所述深冷节流阀5的出口与所述深冷分离精馏塔6入口相连，所述深冷分离精馏塔6的塔底与所述LNG储罐10相连接，所述深冷分离精馏塔塔顶冷凝器8的出口与所述深冷分离精馏塔塔顶分离器9相连，所述深冷分离精馏塔塔顶分离器9的气相出口依次与所述煤层气三级液化换热器4、所述煤层气二级液化换热器3、所述煤层气一级液化换热器2及所述煤层气预冷换热器1连接后与所述尾气燃烧模块相连接。
所述尾气燃烧模块130包括尾气燃烧器14，所述尾气燃烧器14包含空气入口和尾气入口，所述尾气燃烧器14燃烧产物出口与所述塔底重沸器15相连。
在一些较佳的实施例中，尾气燃烧器14中助燃流体为空气。
以下进一步说明上述从含氧煤层气中回收甲烷的系统10的工作原理。
净化后的含氧煤层气(只含有甲烷、氮气、氧气)经过煤层气预冷换热器1、煤层气一级液化换热器2、煤层气二级液化换热器3以及煤层气三级液化换热器4与冷流的不断换热降温，然后经过深冷节流阀5进一步降温，其后进入深冷分离精馏塔6，在深冷分离精馏塔6在深冷分离精馏塔塔顶冷凝器8和深冷分离精馏塔重沸器7的作用下不断进行传热传质，塔底分离出甲烷含量95％以上的LNG产品。深冷分离精馏塔塔顶分离器9气相端尾气中含有15％浓度以上的甲烷从而以保证后期尾气冷量回收过程的安全。
深冷分离精馏塔塔顶分离器9气相端产出尾气依次通过煤层气三级液化换热器4、煤层气二级液化换热器3、煤层气一级液化换热器2以及煤层气预冷换热器1进行尾气中冷量回收，回收冷量后的尾气进入尾气燃烧器14与空气混合进行充分燃烧，为制冷精馏塔16的塔底重沸器15提供热量。
吸收式制冷系统包括的吸收式制冷剂在制冷精馏塔16内不断传热传质，在一次分离器18气相端产生纯度高达99％的制冷剂浓溶液，制冷剂浓溶液经过冷凝器19以及吸收式制冷预冷换热器20不断降温，然后在吸收式制冷节流阀21的作用下节流降温达到所需制冷温度(优选的制冷温度为-30℃)，达到制冷温度的浓吸收式制冷剂溶液一部分为吸收式制冷预冷换热器20中的热流的温降提供冷量，另一部分为煤层气预冷换热器1中的热流的温降提供冷量。完成供冷后的吸收式制冷剂浓溶液与换热后的塔底产出的吸收式制冷剂稀溶液混合，混合后的吸收式制冷剂溶液经过回热冷凝器22、制冷剂溶液泵23升压后，通过吸收式制冷回热换热器24与塔底产出的吸收式制冷剂稀溶液进行热交换升温后进入吸收式制冷精馏塔16完成整个循环。
混合冷剂制冷液化系统包括的混合制冷剂经过压缩机11和冷凝器12的压缩、冷凝作用一次通过煤层气预冷换热器1、煤层气一级液化换热器2及煤层气二级液化换热器3与换热器中冷流的不断换热降温，然后与深冷分离精馏塔6、深冷分离精馏塔重沸器7进行换热，充分利用深冷分离精馏塔重沸器7中的冷量，实现温降，与深冷分离精馏塔重沸器7实现冷量回收后的混合制冷剂经过煤层气三级换热器4与其中冷流换热实现进一步温降，然后经过混合冷剂节流阀13节流降温后达到所需制冷温度要求，达到制冷温度需求的混合制冷剂经过精馏塔塔顶冷凝器8为精馏塔提供冷量，然后依次经过煤层气三级液化换热器4、煤层气二级液化换热器3和煤层气一级液化换热器2提供换热器换热所需冷量后完成循环。
可以理解，在上述整个工艺中，通过调整尾气燃烧器14中助燃流体(空气)的流量实现尾气的充分燃烧，尾气燃烧系统为制冷精馏塔16的塔底重沸器15提供热量，由于利用塔底重沸器15冷能实现煤层气的液化过程的温降，充分利用制冷精馏塔16上端的氮氧尾气冷量回收完后燃烧过程的产热为预冷循环提供所需的热量，节能环保。
本发明提供的从含氧煤层气中回收甲烷的系统，可以在不脱除氧气的前提下，保证整个甲烷回收过程的安全，并能够充分利用尾气中的甲烷资源来降低整个系统的能耗，实现节能。
当然本发明的从含氧煤层气中回收甲烷的系统还可具有多种变换及改型，并不局限于上述实施方式的具体结构。总之，本发明的保护范围应包括那些对于本领域普通技术人员来说显而易见的变换或替代以及改型。

Claims (7)

1.一种从含氧煤层气中回收甲烷的系统，其特征在于，包括：制冷模块、深冷分离储存模块、尾气燃烧模块；其中：
所述制冷模块包括吸收式制冷预冷单元以及混合制冷剂制冷液化单元；
所述吸收式制冷预冷单元包括塔底重沸器、制冷精馏塔、塔顶冷凝器、一次分离器、冷凝器、吸收式制冷预冷换热器、吸收式制冷预冷节流阀、回热冷凝器、制冷剂溶液泵、吸收式制冷回热换热器及吸收式制冷回热节流阀，所述制冷精馏塔、塔顶冷凝器、一次分离器、冷凝器、预冷换热器及吸收式制冷节流阀通过管道依次连接，所述吸收式制冷节流阀通过管道依次经所述吸收式制冷预冷换热器、回热冷凝器、制冷剂溶液泵及吸收式制冷回热换热器连接所述制冷精馏塔，所述塔底重沸器连接于所述制冷精馏塔的下方，且所述塔底重沸器的一端通过管道依次经所述连接吸收式制冷回热换热器、所述吸收式制冷回热节流阀连接所述制冷精馏塔；
所述混合冷剂制冷液化单元包括由混合冷剂压缩机及混合冷剂冷凝器组成的压缩机组件、混合冷剂节流阀、煤层气预冷换热器、煤层气一级液化换热器、煤层气二级液化换热器、煤层气三级液化换热器，所述混合冷剂压缩机入口连接所述煤层气一级液化换热器的制冷剂出口，所述混合冷剂压缩机出口连接所述混合冷剂冷凝器入口，所述混合冷剂冷凝器出口依次连接所述煤层气预冷换热器、所述煤层气一级液化换热器及所述煤层气二级液化换热器，所述煤层气二级液化换热器的制冷剂出口与所述塔底重沸器制冷剂入口相连，所述塔底重沸器制冷剂出口与所述煤层气三级液化换热器制冷剂入口相连，所述煤层气三级液化换热器制冷剂出口与所述混合冷剂节流阀入口相连，所述混合冷剂节流阀出口与塔顶冷凝器相连，所述塔顶冷凝器制冷剂出口依次与所述煤层气三级液化换热器、所述煤层气二级液化换热器、所述煤层气一级液化换热器相连，实现循环；
所述深冷分离储存模块包括深冷节流阀、深冷分离精馏塔、深冷分离精馏塔塔顶冷凝器、深冷分离精馏塔塔顶分离器、深冷分离精馏塔重沸器及LNG储罐，所述深冷节流阀的入口与所述煤层气三级液化换热器、煤层气二级液化换热器、煤层气一级液化换热器及煤层气预冷换热器分别连接，所述深冷节流阀的出口与所述深冷分离精馏塔入口相连，所述深冷分离精馏塔的塔底与所述LNG储罐相连接，所述深冷分离精馏塔塔顶冷凝器的出口与所述深冷分离精馏塔塔顶分离器相连，所述深冷分离精馏塔塔顶分离器的气相出口依次与所述煤层气三级液化换热器、所述煤层气二级液化换热器、所述煤层气一级液化换热器及所述煤层气预冷换热器连接后与所述尾气燃烧模块相连接；
所述尾气燃烧模块包括尾气燃烧器，所述尾气燃烧器包含空气入口和尾气入口，所述尾气燃烧器燃烧产物出口与所述塔底重沸器相连。
2.如权利要求1所述的从含氧煤层气中回收甲烷的系统，其特征在于，所述吸收式制冷预冷单元包括的吸收式制冷剂为氨-水制冷剂。
3.如权利要求1所述的从含氧煤层气中回收甲烷的系统，其特征在于，所述混合制冷剂制冷液化单元包括的混合制冷剂为天然制冷剂，所述天然制冷剂为由氮气、甲烷、乙烷、丙烷、异丁烷和戊丁烷以任意配比组成的混合物。
4.如权利要求1所述的从含氧煤层气中回收甲烷的系统，其特征在于，所述压缩机组件包括至少一对所述混合冷剂压缩机及混合冷剂冷凝器的组合。
5.如权利要求4所述的从含氧煤层气中回收甲烷的系统，其特征在于，所述压缩机组件中包括三对所述混合冷剂压缩机及混合冷剂冷凝器的组合。
6.如权利要求1所述的从含氧煤层气中回收甲烷的系统，其特征在于，经所述精馏塔塔顶尾气中甲烷含量高于爆炸上限接。
7.如权利要求1所述的从含氧煤层气中回收甲烷的系统，其特征在于，所述含氧煤层气由甲烷、氮气及氧气组成。
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