CN212299664U - 一种天然气液化和凝液回收集成装置 - Google Patents

一种天然气液化和凝液回收集成装置 Download PDF

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CN212299664U
CN212299664U CN202021771102.0U CN202021771102U CN212299664U CN 212299664 U CN212299664 U CN 212299664U CN 202021771102 U CN202021771102 U CN 202021771102U CN 212299664 U CN212299664 U CN 212299664U
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heavy hydrocarbon
pipeline
cold box
natural gas
liquefaction
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王科
韩淑怡
李莹珂
郑春来
蒋志明
蒲黎明
周璇
尹奎
汪贵
田静
陈运强
赵雨亮
李嘉迪
杨苗
陈凯文
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
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China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
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Abstract

本实用新型公开了一种天然气液化和凝液回收集成装置，包括液化冷箱、脱重烃塔、脱重烃塔回流罐以及凝液回收单元，液化冷箱与天然气管道和脱重烃塔连接，脱重烃塔的顶部气相出口与液化冷箱连接，液化冷箱与脱重烃塔回流罐连接，脱重烃塔回流罐的液相出口通过设置有脱重烃塔回流泵的管道与脱重烃塔上部连接，凝液回收单元用于对脱重烃后的天然气进一步回收重烃，并将处理后的天然气送回液化冷箱的冷凝段。本实用新型采用脱重烃塔脱除天然气中的C5 +重烃组成，以避免天然气液化过程中设备和管道冻堵，而且通过凝液回收单元对脱重烃后的天然气提取乙烷、丙烷、丁烷等组成。本实用新型除了适用于天然气之外，还适用于煤层气、焦炉煤气等烃类混合物的一种或多种。

Description

一种天然气液化和凝液回收集成装置
技术领域
本实用新型属于天然气液化和天然气凝液回收技术领域，特别涉及一种天然气液化和凝液回收集成装置。
背景技术
天然气中甲烷占绝大多数，另有少量的乙烷、丙烷和丁烷，以及微量的戊烷、己烷等组分。天然气凝液回收是指将天然气中的乙烷、丙烷、丁烷、戊烷等组成从天然气中分离出来，将回收后的凝液用于化工原料，具有较好的经济效益。天然气液化是将净化处理后的天然气经过低温冷凝、液化后生产液化天然气。由于天然气中含有重烃组分，重烃组分是指C5 +烃类，因重烃熔沸点低，在低温环境下冷凝、冻结而堵塞管道和设备，因此天然气在液化过程中必须脱除所含的重烃组分，以避免天然气在液化过程中引起冻堵，脱除重烃后的天然气进一步冷凝、液化生产液化天然气。
而且天然气液化工厂需要补充乙烷、丙烷等制冷剂，因此可以在脱重烃塔后设置凝液回收单元从天然气中提取乙烷、丙烷等组成用于制冷剂补充。同时，已经建成的天然气液化工程可以通过降低液化天然气产品中的高位热值(HHV)以最低的边际成本提取乙烷、丙烷、丁烷等组成，可以在脱重烃塔后增加凝液回收装置，以最小的投资以最低的成本生产乙烷、丙烷、丁烷等产品。
实用新型内容
本实用新型的发明目的在于：针对上述存在的问题，提供一种能够避免天然气液化过程中设备和管道冻堵，并能对脱重烃后的天然气提取乙烷、丙烷、丁烷等组成的天然气液化和凝液回收集成装置。
本实用新型采用的技术方案是：一种天然气液化和凝液回收集成装置，其特征在于：包括液化冷箱、脱重烃塔、脱重烃塔回流罐以及凝液回收单元，所述液化冷箱内的一级预冷段进口端与天然气进气管道连接，其出口端通过管道与脱重烃塔连接，经脱重烃塔分离后的液烃通过底部管道进入后工序，所述脱重烃塔的顶部气相出口通过管道与液化冷箱内的二级预冷段进口端连接，所述二级预冷段的出口端通过管道与脱重烃塔回流罐连接，所述脱重烃塔回流罐的液相出口通过设置有脱重烃塔回流泵的管道与脱重烃塔上部连接，所述脱重烃塔回流罐的气相出口分为两路，一路通过设置有第一节流阀的管道与液化冷箱内的冷凝段进口端连接，所述冷凝段的出口端通过管道至后工序，另一路通过管道与凝液回收单元连接，所述凝液回收单元用于对脱重烃后的天然气进一步回收重烃，并将处理后的天然气送回液化冷箱的冷凝段。
本实用新型所述的天然气液化和凝液回收集成装置，其所述液化冷箱与冷剂制冷单元连接，所述冷剂制冷单元包括第一冷却器和冷剂压缩机，所述第一冷却器与液化冷箱内的冷却段连接，所述冷却段通过设置有第二节流阀的管道与液化冷箱内的复热段连接，所述复热段通过管道与冷剂压缩机连接，所述冷剂压缩机通过管道与第一冷却器连接，形成冷剂制冷循环回路。
本实用新型所述的天然气液化和凝液回收集成装置，其所述凝液回收单元包括重烃回收冷箱、低温分离器以及脱甲烷塔，所述脱重烃塔回流罐的一路气相通过管道与重烃回收冷箱内的一级预冷段进口端连接，所述重烃回收冷箱内的一级预冷段出口端通过管道与低温分离器连接，所述低温分离器的底部液相出口通过设置有第三节流阀的管道与脱甲烷塔连接，所述低温分离器的顶部气相出口分为两路，一路通过管道与重烃回收冷箱内的二级预冷段进口端连接，所述重烃回收冷箱内的二级预冷段出口端通过设置有第四节流阀的管道与脱甲烷塔上部连接，另一路经膨胀机膨胀后通过管道与脱甲烷塔连接，所述脱甲烷塔的顶部气相出口通过管道与重烃回收冷箱内的复热段进口端连接，所述重烃回收冷箱内的复热段出口端通过管道依次与膨胀机和干气压缩机连接，并经第二冷却器冷却后送回重烃回收冷箱进一步冷却，冷却后的气相通过管道与液化冷箱内的冷凝段进口端连接。
本实用新型所述的天然气液化和凝液回收集成装置，其所述脱甲烷塔顶部的气相在经过第二冷却器冷却后分为两路，一路送回重烃回收冷箱，另一路通过管道与重烃回收冷箱内的冷却段进口端连接，所述重烃回收冷箱内的冷却段出口端通过设置有第五节流阀的管道与脱甲烷塔上部连接。
本实用新型所述的天然气液化和凝液回收集成装置，其所述脱甲烷塔中部液相出口通过管道与重烃回收冷箱内的加热段进口端连接，所述重烃回收冷箱内的加热段出口端通过管道与脱甲烷塔中部液相入口连接。
本实用新型所述的天然气液化和凝液回收集成装置，其所述脱甲烷塔的下部液相出口通过设置有脱甲烷塔重沸器的管道与脱甲烷塔的下部液相入口连接。
与现有技术相比，本实用新型的积极效果是：采用脱重烃塔脱除天然气中的C5 +重烃组成，以避免天然气液化过程中设备和管道冻堵，而且通过设置凝液回收单元对脱重烃后的天然气提取乙烷、丙烷、丁烷等组成，凝液回收单元后的天然气进一步冷凝液化生产液化天然气，并能实现天然气液化在有无凝液回收单元的情况下灵活切换。本实用新型除了适用于天然气之外，还能适用于煤层气、焦炉煤气等烃类混合物的一种或多种。
附图说明
本实用新型将通过具体实施例并参照附图的方式说明，其中
图1为本实用新型实施例1的原理示意图。
图2为本实用新型实施例2的原理示意图。
图中标记：1为天然气进气管道，2为液化冷箱，4为脱重烃塔，7为脱重烃塔回流罐，9为脱重烃塔回流泵，12为第一节流阀，18为第二节流阀，21为冷剂压缩机，23为第一冷却器，25为重烃回收冷箱，27为低温分离器，29为第三节流阀，31为脱甲烷塔，33为膨胀机，37为第四节流阀，42为干气压缩机，44为第二冷却器，49为第五节流阀，54为脱甲烷塔重沸器。
具体实施方式
为使本实用新型实施例的目的、技术方案和优点更加清楚，下面将结合本实用新型实施例中的附图，对本实用新型实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本实用新型一部分实施例，而不是全部的实施例。通常在此处附图中描述和示出的本实用新型实施例的组件可以以各种不同的配置来布置和设计。
因此，以下对在附图中提供的本实用新型的实施例的详细描述并非旨在限制要求保护的本实用新型的范围，而是仅仅表示本实用新型的选定实施例。基于本实用新型中的实施例，本领域普通技术人员在没有作出创造性劳动前提下所获得的所有其他实施例，都属于本实用新型保护的范围。
需要说明的是，在不冲突的情况下，本实用新型中的实施例及实施例中的特征可以相互组合。
应注意到：相似的标号和字母在下面的附图中表示类似项，因此，一旦某一项在一个附图中被定义，则在随后的附图中不需要对其进行进一步定义和解释。
在本实用新型实施例的描述中，需要说明的是，指示方位或位置关系为基于附图所示的方位或位置关系，或者是该实用新型产品使用时惯常摆放的方位或位置关系，或者是本领域技术人员惯常理解的方位或位置关系，或者是该实用新型产品使用时惯常摆放的方位或位置关系，仅是为了便于描述本实用新型和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本实用新型的限制。此外，术语“第一”、“第二”仅用于区分描述，而不能理解为指示或暗示相对重要性。
在本实用新型实施例的描述中，还需要说明的是，除非另有明确的规定和限定，术语“设置”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是直接连接，也可以通过中间媒介间接连接。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本实用新型中的具体含义；实施例中的附图用以对本实用新型实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本实用新型一部分实施例，而不是全部的实施例。通常在此处附图中描述和示出的本实用新型实施例的组件可以以各种不同的配置来布置和设计。
实施例1：
如图1所示，一种天然气液化和凝液回收集成装置，包括液化冷箱2、脱重烃塔4、脱重烃塔回流罐7以及凝液回收单元，所述液化冷箱2内的一级预冷段进口端与天然气进气管道1连接，其出口端通过管道与脱重烃塔4连接，经脱重烃塔4分离后的液烃通过底部管道进入后工序，所述脱重烃塔4的顶部气相出口通过管道与液化冷箱2内的二级预冷段进口端连接，所述二级预冷段的出口端通过管道与脱重烃塔回流罐7连接，所述脱重烃塔回流罐7的液相出口通过设置有脱重烃塔回流泵9的管道与脱重烃塔4上部连接，所述脱重烃塔回流罐7的气相出口分为两路，一路通过设置有第一节流阀12的管道与液化冷箱2内的冷凝段进口端连接，所述冷凝段的出口端通过管道至后工序，另一路通过管道与凝液回收单元连接，所述凝液回收单元用于对脱重烃后的天然气进一步回收重烃，并将处理后的天然气送回液化冷箱2的冷凝段。
其中，所述液化冷箱2与冷剂制冷单元连接，所述冷剂制冷单元包括第一冷却器23和冷剂压缩机21，所述第一冷却器23与液化冷箱2内的冷却段连接，所述冷却段通过设置有第二节流阀18的管道与液化冷箱2内的复热段连接，所述复热段通过管道与冷剂压缩机21连接，所述冷剂压缩机21通过管道与第一冷却器23连接，形成冷剂制冷循环回路。
在本实施例中，所述凝液回收单元包括重烃回收冷箱25、低温分离器27以及脱甲烷塔31，所述脱重烃塔回流罐7的一路气相通过管道与重烃回收冷箱25内的一级预冷段进口端连接，所述重烃回收冷箱25内的一级预冷段出口端通过管道与低温分离器27连接，所述低温分离器27的底部液相出口通过设置有第三节流阀29的管道与脱甲烷塔31连接，所述低温分离器27的顶部气相出口分为两路，一路通过管道与重烃回收冷箱25内的二级预冷段进口端连接，所述重烃回收冷箱25内的二级预冷段出口端通过设置有第四节流阀37的管道与脱甲烷塔31上部连接，另一路经膨胀机33膨胀后通过管道与脱甲烷塔31连接，所述脱甲烷塔31的顶部气相出口通过管道与重烃回收冷箱25内的复热段进口端连接，所述重烃回收冷箱25内的复热段出口端通过管道依次与膨胀机33和干气压缩机42连接，并经第二冷却器44冷却后送回重烃回收冷箱25进一步冷却，冷却后的气相通过管道与液化冷箱2内的冷凝段进口端连接。
所述脱甲烷塔31中部液相出口通过管道与重烃回收冷箱25内的加热段进口端连接，所述重烃回收冷箱25内的加热段出口端通过管道与脱甲烷塔31中部液相入口连接；所述脱甲烷塔31的下部液相出口通过设置有脱甲烷塔重沸器54的管道与脱甲烷塔31的下部液相入口连接。
基于上述天然气液化和凝液回收集成装置，其天然气液化和凝液回收集成的方法，具体包括如下步骤：
第一步，来自天然气进气管道的4000kPa.a～6000kPa.a，30～50℃的天然气进入液化冷箱预冷至-25～-45℃后进入脱重烃塔下部进行分离，脱重烃塔底部液烃进入下一工序处理，脱重烃塔顶部气相进入液化冷箱预冷至-50～-65℃后进入脱重烃塔回流罐进行气液分离，其中：液相通过脱重烃塔回流泵增压后进入脱重烃塔顶部，气相按照任意比例分为两路，这样能够实现天然气液化和凝液回收的灵活切换，当不需要进行凝液回收时，气相全部经过第一节流阀进入液化冷箱；当需要进行凝液回收时，可以根据需求控制气相全部进入或者部分进入重烃回收冷箱，具体地，其中一路经第一节流阀节流至3500kPa.a～5500kPa.a进入液化冷箱进一步冷凝至-150～-162℃后进入下一步工序处理；另一路进入重烃回收冷箱预冷至-50～-70℃后进一步回收重烃。
第二步，进入重烃回收冷箱预冷至-50～-70℃后进入低温分离器进行气液分离，其中：液相通过第三节流阀节流至1000kPa.a～3500kPa.a后进入脱甲烷塔中部，气相分为两路，一路1％～30％物流进入重烃回收冷箱冷却至-95～-125℃进入第四节流阀节流至1000kPa.a～3500kPa.a后进入脱甲烷塔上部，另一路70～99％物流进入膨胀机膨胀至1000kPa.a～3500kPa.a后进入脱甲烷塔中上部；脱甲烷塔顶部出口的气相进入重烃回收冷箱复热至25～40℃，经过膨胀机增压后进入干气压缩机增压至4000kPa.a～6000kPa.a进入第二冷却器冷却至40～50℃，冷却后的气相进入重烃回收冷箱冷却至-20～-40℃后进入液化冷箱液化。
其中，脱甲烷塔中部液相进入重烃回收冷箱加热后返回脱甲烷塔中部入口，回收脱甲烷塔中的冷量，脱甲烷塔下部液相进入脱甲烷塔重沸器加热后返回脱甲烷塔下部入口，进行控制脱甲烷塔底液相中甲烷的含量，脱甲烷塔底部液相进入下一工序处理。
第三步、自第一冷却器来的冷剂进入液化冷箱冷却至-150～-162℃，通过管道进入第二节流阀节流至300～500kPa.a进入液化冷箱复热至35～45℃，经管道进入冷剂压缩机增压至3500kPa.a～5000kPa.a，进入第一冷却器冷却至40～50℃后进入液化冷箱，形成冷剂制冷循环为液化冷箱提供所需冷量。
实施例2：
如图2所示，实施例2与实施例1基本相同，其主要的区别在于：所述脱甲烷塔31顶部的气相在经过第二冷却器44冷却后分为两路，一路送回重烃回收冷箱25，另一路通过管道与重烃回收冷箱25内的冷却段进口端连接，所述重烃回收冷箱25内的冷却段出口端通过设置有第五节流阀49的管道与脱甲烷塔31上部连接。
基于上述结构设计的不同，其天然气液化和凝液回收集成方法的主要区别在于：在第二步中，脱甲烷塔顶部出口的气相经第二冷却器冷却后分为两路，其中一路80～95％物流进入重烃回收冷箱冷却至-20～-40℃后进入液化冷箱液化，另一路5～20％物流进入重烃回收冷箱冷却至-95～-125℃，进入第五节流阀节流至1000kPa.a～3500kPa.a后进入脱甲烷塔顶部。
本实用新型并不局限于前述的具体实施方式。本实用新型扩展到任何在本说明书中披露的新特征或任何新的组合，以及披露的任一新的方法或过程的步骤或任何新的组合。

Claims (6)

1.一种天然气液化和凝液回收集成装置，其特征在于：包括液化冷箱(2)、脱重烃塔(4)、脱重烃塔回流罐(7)以及凝液回收单元，所述液化冷箱(2)内的一级预冷段进口端与天然气进气管道(1)连接，其出口端通过管道与脱重烃塔(4)连接，经脱重烃塔(4)分离后的液烃通过底部管道进入后工序，所述脱重烃塔(4)的顶部气相出口通过管道与液化冷箱(2)内的二级预冷段进口端连接，所述二级预冷段的出口端通过管道与脱重烃塔回流罐(7)连接，所述脱重烃塔回流罐(7)的液相出口通过设置有脱重烃塔回流泵(9)的管道与脱重烃塔(4)上部连接，所述脱重烃塔回流罐(7)的气相出口分为两路，一路通过设置有第一节流阀(12)的管道与液化冷箱(2)内的冷凝段进口端连接，所述冷凝段的出口端通过管道至后工序，另一路通过管道与凝液回收单元连接，所述凝液回收单元用于对脱重烃后的天然气进一步回收重烃，并将处理后的天然气送回液化冷箱(2)的冷凝段。
2.根据权利要求1所述的天然气液化和凝液回收集成装置，其特征在于：所述液化冷箱(2)与冷剂制冷单元连接，所述冷剂制冷单元包括第一冷却器(23)和冷剂压缩机(21)，所述第一冷却器(23)与液化冷箱(2)内的冷却段连接，所述冷却段通过设置有第二节流阀(18)的管道与液化冷箱(2)内的复热段连接，所述复热段通过管道与冷剂压缩机(21)连接，所述冷剂压缩机(21)通过管道与第一冷却器(23)连接，形成冷剂制冷循环回路。
3.根据权利要求1或2所述的天然气液化和凝液回收集成装置，其特征在于：所述凝液回收单元包括重烃回收冷箱(25)、低温分离器(27)以及脱甲烷塔(31)，所述脱重烃塔回流罐(7)的一路气相通过管道与重烃回收冷箱(25)内的一级预冷段进口端连接，所述重烃回收冷箱(25)内的一级预冷段出口端通过管道与低温分离器(27)连接，所述低温分离器(27)的底部液相出口通过设置有第三节流阀(29)的管道与脱甲烷塔(31)连接，所述低温分离器(27)的顶部气相出口分为两路，一路通过管道与重烃回收冷箱(25)内的二级预冷段进口端连接，所述重烃回收冷箱(25)内的二级预冷段出口端通过设置有第四节流阀(37)的管道与脱甲烷塔(31)上部连接，另一路经膨胀机(33)膨胀后通过管道与脱甲烷塔(31)连接，所述脱甲烷塔(31)的顶部气相出口通过管道与重烃回收冷箱(25)内的复热段进口端连接，所述重烃回收冷箱(25)内的复热段出口端通过管道依次与膨胀机(33)和干气压缩机(42)连接，并经第二冷却器(44)冷却后送回重烃回收冷箱(25)进一步冷却，冷却后的气相通过管道与液化冷箱(2)内的冷凝段进口端连接。
4.根据权利要求3所述的天然气液化和凝液回收集成装置，其特征在于：所述脱甲烷塔(31)顶部的气相在经过第二冷却器(44)冷却后分为两路，一路送回重烃回收冷箱(25)，另一路通过管道与重烃回收冷箱(25)内的冷却段进口端连接，所述重烃回收冷箱(25)内的冷却段出口端通过设置有第五节流阀(49)的管道与脱甲烷塔(31)上部连接。
5.根据权利要求3所述的天然气液化和凝液回收集成装置，其特征在于：所述脱甲烷塔(31)中部液相出口通过管道与重烃回收冷箱(25)内的加热段进口端连接，所述重烃回收冷箱(25)内的加热段出口端通过管道与脱甲烷塔(31)中部液相入口连接。
6.根据权利要求3所述的天然气液化和凝液回收集成装置，其特征在于：所述脱甲烷塔(31)的下部液相出口通过设置有脱甲烷塔重沸器(54)的管道与脱甲烷塔(31)的下部液相入口连接。
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CN111964353B (zh) * 2020-08-20 2023-10-27 中国石油集团工程股份有限公司 一种天然气液化和凝液回收集成装置和方法

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