CN111981768A - 一种天然气低温节流提取氦气装置和方法 - Google Patents

一种天然气低温节流提取氦气装置和方法 Download PDF

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CN111981768A
CN111981768A CN202010842142.8A CN202010842142A CN111981768A CN 111981768 A CN111981768 A CN 111981768A CN 202010842142 A CN202010842142 A CN 202010842142A CN 111981768 A CN111981768 A CN 111981768A
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pipeline
cold box
natural gas
enters
kpa
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王科
韩淑怡
蒲黎明
李莹珂
杜娟
陈运强
刘玉洁
尹奎
陈凯文
杨苗
李嘉迪
赵雨亮
乔研佳
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
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Abstract

本发明公开了一种天然气低温节流提取氦气装置和方法，包括冷箱以及闪蒸罐，所述冷箱与天然气进气管道连接，所述冷箱与闪蒸罐连接，所述闪蒸罐的顶部气相出口与冷箱连接，所述闪蒸罐的底部液相出口与一级增压泵连接，经一级增压泵增压后分为两路，其中一路经二级增压泵增压后通过管道与冷箱连接，另一路通过管道与冷箱连接，并经冷箱复热后，通过管道与膨胀机的膨胀端连接，经膨胀后通过管道与冷箱连接，并经冷箱复热后，通过管道与膨胀机的增压端连接，经增压后通过管道与冷却单元连接。本发明通过天然气低温节流实现天然气中氦气提浓并回收，采用液烃节流和天然气膨胀为装置提供冷量，不需要外部制冷提供冷量，实现冷量优化匹配，降低了装置能耗。

Description

一种天然气低温节流提取氦气装置和方法
技术领域
本发明属于天然气处理技术领域，特别涉及一种天然气低温节流提取氦气装置和方法，适用于从含有氦气的天然气提取氦气。
背景技术
氦气在常温下是一种极轻的无色、无臭、无味的单原子气体，也是所有气体中最难液化的，其常温下液化温度达到-268.9℃。氦气在医疗、光纤、超导领域具有广泛的用途。目前工业上含有氦气的天然气是生产氦气唯一来源。天然气中氦气含量最低仅0.05％，最高可以达到8％。利用氦气和天然气沸点的不同，低温精馏提氦技术仍是从天然气中提取氦气的主要方式，该技术是在低温下采用一个或两个精馏塔将天然气中的氦气富集提浓。采用精馏塔低温分离提取氦气能够有效提浓氦气，工艺流程相对复杂，投资较高。
发明内容
本发明的目的在于：针对上述存在的问题，提供一种能够实现冷量优化匹配，降低能耗的天然气低温节流提取氦气装置和方法。
本发明采用的技术方案是：一种天然气低温节流提取氦气装置，其特征在于：包括冷箱以及闪蒸罐，所述冷箱与天然气进气管道连接，所述冷箱通过设置有第一节流阀的管道与闪蒸罐连接，所述闪蒸罐的顶部气相出口通过管道与冷箱连接，所述闪蒸罐的底部液相出口通过管道与一级增压泵连接，经一级增压泵增压后分为两路，其中一路经二级增压泵增压后通过管道与冷箱连接，并经冷箱复热后通过管道送至后工序，另一路通过管道与冷箱连接，并经冷箱复热后，通过管道与膨胀机的膨胀端连接，经膨胀后通过管道与冷箱连接，并经冷箱复热后，通过管道与膨胀机的增压端连接，经增压后通过管道与冷却单元连接，经冷却后通过管道送至后工序。
本发明所述的天然气低温节流提取氦气装置，其所述闪蒸罐的顶部气相在冷箱内冷凝后，通过管道与分离罐连接，所述分离罐顶部的气相出口通过管道与冷箱连接，经冷箱复热后通过管道送至后工序，所述分离罐底部的液相出口通过设置有第二节流阀的管道与冷箱连接，经冷箱复热后通过管道送至后工序。
本发明所述的天然气低温节流提取氦气装置，其所述分离罐底部的液相经冷箱复热后通过管道与燃料气压缩机连接，所述燃料气压缩机通过管道与第三冷却器连接，经冷却后通过管道送至后工序。
本发明所述的天然气低温节流提取氦气装置，其所述冷却单元包括第一冷却器、天然气压缩机和第二冷却器，所述膨胀机的增压端通过管道与第一冷却器连接，所述第一冷却器通过管道与天然气压缩机连接，所述天然气压缩机通过管道与第二冷却器连接，所述第二冷却器通过管道送至后工序。
本发明所述的天然气低温节流提取氦气装置，其所述冷箱内的预冷段出口端通过管道与脱重烃塔连接，所述脱重烃塔的顶部气相出口通过管道与冷箱内的二次预冷段进口端连接，所述冷箱内的二次预冷段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气相通过管道与冷箱内的冷凝段连接。
本发明所述的天然气低温节流提取氦气装置，其所述脱重烃塔回流罐的底部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，所述脱重烃塔底部液烃通过管道至后工序。
一种天然气低温节流提取氦气方法，其特征在于：所述方法具体为：将来自天然气进气管道的天然气进入冷箱预冷至-145～-125℃后，通过管道经第一节流阀节流至450kPa.a～650kPa.a，并经管道送至闪蒸罐进行气液分离，其中：液相通过管道进入一级增压泵增压至1500kPa.a～2000kPa.a后分为两路物流，其中：一股40％～60％物流通过管道经过二级增压泵增压至5500kPa.a～6500kPa.a后，经过管道进入冷箱复热到25～45℃，再经管道进入下一工序处理；另一股40～60％物流通过管道进入冷箱复热至-70～-60℃，再通过管道进入膨胀机膨胀至600kPa.a～1200kPa.a后，经管道返回冷箱进一步复热至25～45℃，经过管道进入膨胀机增压后，通过冷却单元冷却并送至下一工序处理；所述闪蒸罐中的气相通过管道送至冷箱进一步冷凝。
本发明所述的天然气低温节流提取氦气方法，其所述闪蒸罐的气相至冷箱进一步冷凝至-176～-170℃后，经过管道进入分离罐进行气液分离，其中：气相通过管道进入冷箱复热至25～45℃后，经过管道至下一工序处理；液相通过管道进入第二节流阀节流至200kPa.a～300kPa.a后，经过管道进入冷箱复热至25～45℃后，通过管道进入燃料气压缩机增压至500kPa.a～700kPa.a后，经过管道至第三冷却器冷却至40～50℃后送至下一工序处理。
本发明所述的天然气低温节流提取氦气方法，其经膨胀机增压后的物料通过管道送至第一冷却器冷却至40～50℃，然后通过管道进入天然气压缩机增压至5600kPa.a～6600kPa.a后，通过管道经过第二冷却器冷却至40～50℃后，再通过管道送至下一工序处理。
本发明所述的天然气低温节流提取氦气方法，其来自天然气进气管道的天然气进入冷箱预冷至-65～-55℃后，经管道进入脱重烃塔下部进行分离，脱重烃塔底部液烃经过管道进入下一工序处理；脱重烃塔顶部气相通过管道进入冷箱预冷至-75～-65℃后，通过管道进入脱重烃塔回流罐进行气液分离，其中：液相通过管道进入脱重烃塔回流泵增压5200kPa.a～6200kPa.a后，经过管道进入脱重烃塔顶部，气相通过管道进入冷箱进一步冷凝。
与现有技术相比，本发明的积极效果是：通过天然气低温节流实现天然气中氦气提浓并回收，采用液烃节流和天然气膨胀为装置提供冷量，不需要外部制冷提供冷量，实现冷量优化匹配，降低了装置能耗。
附图说明
本发明将通过具体实施例并参照附图的方式说明，其中
图1为本发明实施例1的原理示意图。
图2为本发明实施例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，14为第一节流阀，16为闪蒸罐，19为分离罐，23为第二节流阀，27为一级增压泵，29为二级增压泵，34为膨胀机，38为第一冷却器，40为天然气压缩机，42为第二冷却器，44为燃料压缩机，46为第三冷却器。
具体实施方式
为使本发明实施例的目的、技术方案和优点更加清楚，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，所描述的实施例是本发明一部分实施例，而不是全部的实施例。通常在此处附图中描述和示出的本发明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发明的实施例的详细描述并非旨在限制要求保护的本发明的范围，而是仅仅表示本发明的选定实施例。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，都属于本发明保护的范围。
需要说明的是，在不冲突的情况下，本发明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。
在本发明实施例的描述中，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，或者是该发明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，或者是该发明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发明和简化描述，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发明的限制。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。
在本发明实施例的描述中，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发明中的具体含义；实施例中的附图用以对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本发明一部分实施例，而不是全部的实施例。通常在此处附图中描述和示出的本发明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，一种天然气低温节流提取氦气装置，包括冷箱2以及闪蒸罐16，所述冷箱2与天然气进气管道1连接，所述冷箱2通过设置有第一节流阀14的管道与闪蒸罐16连接，所述闪蒸罐16的顶部气相出口通过管道与冷箱2连接，所述闪蒸罐16的顶部气相在冷箱2内冷凝后，通过管道与分离罐19连接，所述分离罐19顶部的气相出口通过管道与冷箱2连接，经冷箱2复热后通过管道送至后工序，所述分离罐19底部的液相出口通过设置有第二节流阀23的管道与冷箱2连接，经冷箱2复热后通过管道与燃料气压缩机44连接，所述燃料气压缩机44通过管道与第三冷却器46连接，经冷却后通过管道送至后工序；所述闪蒸罐16的底部液相出口通过管道与一级增压泵27连接，经一级增压泵27增压后分为两路，其中一路经二级增压泵29增压后通过管道与冷箱2连接，并经冷箱2复热后通过管道送至后工序，另一路通过管道与冷箱2连接，并经冷箱2复热后，通过管道与膨胀机34的膨胀端连接，经膨胀后通过管道与冷箱2连接，并经冷箱2复热后，通过管道与膨胀机34的增压端连接，经增压后通过管道与冷却单元连接，经冷却后通过管道送至后工序。
其中，所述冷却单元包括第一冷却器38、天然气压缩机40和第二冷却器42，所述膨胀机34的增压端通过管道与第一冷却器38连接，所述第一冷却器38通过管道与天然气压缩机40连接，所述天然气压缩机40通过管道与第二冷却器42连接，所述第二冷却器42通过管道送至后工序。
基于上述天然气低温节流提取氦气装置，本发明还提供一种天然气低温节流提取氦气方法，所述方法具体为：
第一步，将来自天然气进气管道的5000kPa.a～6000kPa.a，30～50℃的天然气进入冷箱预冷至-145～-125℃。
第二步，将冷凝后的天然气通过管道经第一节流阀节流至450kPa.a～650kPa.a，通过节流能够将氦气从液化天然气中闪蒸至气相，实现氦气初步提浓)，并经管道送至闪蒸罐进行气液分离，其中：液相通过管道进入一级增压泵增压至1500kPa.a～2000kPa.a后分为两路物流，其中：一股40％～60％物流通过管道经过二级增压泵增压至5500kPa.a～6500kPa.a后，经过管道进入冷箱复热到25～45℃，再经管道进入下一工序处理；另一股40～60％物流通过管道进入冷箱复热至-70～-60℃，再通过管道进入膨胀机膨胀至600kPa.a～1200kPa.a后，经管道返回冷箱进一步复热至25～45℃，经过管道进入膨胀机增压后，通过冷却单元冷却并送至下一工序处理。
第三步，所述闪蒸罐中的气相通过管道送至冷箱进一步冷凝至-176～-170℃后，经过管道进入分离罐进行气液分离，通过进一步冷凝，将氦气中更多地天然气组分冷凝为液相，实现氦气进一步提浓，其中：气相通过管道进入冷箱复热至25～45℃后，经过管道至下一工序处理；液相通过管道进入第二节流阀节流至200kPa.a～300kPa.a，为来自闪蒸罐的气相进一步冷凝提供冷量，经过管道进入冷箱复热至25～45℃后，通过管道进入燃料气压缩机增压至500kPa.a～700kPa.a后，经过管道至第三冷却器冷却至40～50℃后送至下一工序处理。
具体地，在第二步中，经膨胀机增压后的物料通过管道送至第一冷却器冷却至40～50℃，然后通过管道进入天然气压缩机增压至5600kPa.a～6600kPa.a后，通过管道经过第二冷却器冷却至40～50℃后，再通过管道送至下一工序处理。
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：所述冷箱2内的预冷段出口端通过管道与脱重烃塔4连接，所述脱重烃塔4的顶部气相出口通过管道与冷箱2内的二次预冷段进口端连接，所述冷箱2内的二次预冷段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的气相通过管道与冷箱2内的冷凝段连接；所述脱重烃塔回流罐7的底部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4底部液烃通过管道至后工序。
基于上述结构设计的不同，其天然气低温节流提取氦气方法的主要区别在于：来自天然气进气管道的天然气进入冷箱预冷至-65～-55℃后，经管道进入脱重烃塔下部进行分离，脱重烃塔底部液烃经过管道进入下一工序处理；脱重烃塔顶部气相通过管道进入冷箱进一步预冷至-75～-65℃后，通过管道进入脱重烃塔回流罐进行气液分离，其中：液相通过管道进入脱重烃塔回流泵增压5200kPa.a～6200kPa.a后，经过管道进入脱重烃塔顶部，气相通过管道进入冷箱进一步冷凝至-145～-125℃，后工序与实施例1的第二、三步相同。通过设置脱重烃塔，将天然气中重烃脱除，避免天然气在冷凝过程中冻堵设备或管道。
本发明并不局限于前述的具体实施方式。本发明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 (10)

1.一种天然气低温节流提取氦气装置，其特征在于：包括冷箱(2)以及闪蒸罐(16)，所述冷箱(2)与天然气进气管道(1)连接，所述冷箱(2)通过设置有第一节流阀(14)的管道与闪蒸罐(16)连接，所述闪蒸罐(16)的顶部气相出口通过管道与冷箱(2)连接，所述闪蒸罐(16)的底部液相出口通过管道与一级增压泵(27)连接，经一级增压泵(27)增压后分为两路，其中一路经二级增压泵(29)增压后通过管道与冷箱(2)连接，并经冷箱(2)复热后通过管道送至后工序，另一路通过管道与冷箱(2)连接，并经冷箱(2)复热后，通过管道与膨胀机(34)的膨胀端连接，经膨胀后通过管道与冷箱(2)连接，并经冷箱(2)复热后，通过管道与膨胀机(34)的增压端连接，经增压后通过管道与冷却单元连接，经冷却后通过管道送至后工序。
2.根据权利要求1所述的天然气低温节流提取氦气装置，其特征在于：所述闪蒸罐(16)的顶部气相在冷箱(2)内冷凝后，通过管道与分离罐(19)连接，所述分离罐(19)顶部的气相出口通过管道与冷箱(2)连接，经冷箱(2)复热后通过管道送至后工序，所述分离罐(19)底部的液相出口通过设置有第二节流阀(23)的管道与冷箱(2)连接，经冷箱(2)复热后通过管道送至后工序。
3.根据权利要求2所述的天然气低温节流提取氦气装置，其特征在于：所述分离罐(19)底部的液相经冷箱(2)复热后通过管道与燃料气压缩机(44)连接，所述燃料气压缩机(44)通过管道与第三冷却器(46)连接，经冷却后通过管道送至后工序。
4.根据权利要求1所述的天然气低温节流提取氦气装置，其特征在于：所述冷却单元包括第一冷却器(38)、天然气压缩机(40)和第二冷却器(42)，所述膨胀机(34)的增压端通过管道与第一冷却器(38)连接，所述第一冷却器(38)通过管道与天然气压缩机(40)连接，所述天然气压缩机(40)通过管道与第二冷却器(42)连接，所述第二冷却器(42)通过管道送至后工序。
5.根据权利要求1至4中任意一项所述的天然气低温节流提取氦气装置，其特征在于：所述冷箱(2)内的预冷段出口端通过管道与脱重烃塔(4)连接，所述脱重烃塔(4)的顶部气相出口通过管道与冷箱(2)内的二次预冷段进口端连接，所述冷箱(2)内的二次预冷段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)的气相通过管道与冷箱(2)内的冷凝段连接。
6.根据权利要求5所述的天然气低温节流提取氦气装置，其特征在于：所述脱重烃塔回流罐(7)的底部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(4)底部液烃通过管道至后工序。
7.一种天然气低温节流提取氦气方法，其特征在于：所述方法具体为：将来自天然气进气管道的天然气进入冷箱预冷至-145～-125℃后，通过管道经第一节流阀节流至450kPa.a～650kPa.a，并经管道送至闪蒸罐进行气液分离，其中：液相通过管道进入一级增压泵增压至1500kPa.a～2000kPa.a后分为两路物流，其中：一股40％～60％物流通过管道经过二级增压泵增压至5500kPa.a～6500kPa.a后，经过管道进入冷箱复热到25～45℃，再经管道进入下一工序处理；另一股40～60％物流通过管道进入冷箱复热至-70～-60℃，再通过管道进入膨胀机膨胀至600kPa.a～1200kPa.a后，经管道返回冷箱进一步复热至25～45℃，经过管道进入膨胀机增压后，通过冷却单元冷却并送至下一工序处理；所述闪蒸罐中的气相通过管道送至冷箱进一步冷凝。
8.根据权利要求7所述的天然气低温节流提取氦气方法，其特征在于：所述闪蒸罐的气相至冷箱进一步冷凝至-176～-170℃后，经过管道进入分离罐进行气液分离，其中：气相通过管道进入冷箱复热至25～45℃后，经过管道至下一工序处理；液相通过管道进入第二节流阀节流至200kPa.a～300kPa.a后，经过管道进入冷箱复热至25～45℃后，通过管道进入燃料气压缩机增压至500kPa.a～700kPa.a后，经过管道至第三冷却器冷却至40～50℃后送至下一工序处理。
9.根据权利要求8所述的天然气低温节流提取氦气方法，其特征在于：经膨胀机增压后的物料通过管道送至第一冷却器冷却至40～50℃，然后通过管道进入天然气压缩机增压至5600kPa.a～6600kPa.a后，通过管道经过第二冷却器冷却至40～50℃后，再通过管道送至下一工序处理。
10.根据权利要求9所述的天然气低温节流提取氦气方法，其特征在于：来自天然气进气管道的天然气进入冷箱预冷至-65～-55℃后，经管道进入脱重烃塔下部进行分离，脱重烃塔底部液烃经过管道进入下一工序处理；脱重烃塔顶部气相通过管道进入冷箱预冷至-75～-65℃后，通过管道进入脱重烃塔回流罐进行气液分离，其中：液相通过管道进入脱重烃塔回流泵增压5200kPa.a～6200kPa.a后，经过管道进入脱重烃塔顶部，气相通过管道进入冷箱进一步冷凝。
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