CN106866339B - 一种天然气中回收乙烷联产粗氦的装置及方法 - Google Patents

一种天然气中回收乙烷联产粗氦的装置及方法 Download PDF

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CN106866339B
CN106866339B CN201710223206.4A CN201710223206A CN106866339B CN 106866339 B CN106866339 B CN 106866339B CN 201710223206 A CN201710223206 A CN 201710223206A CN 106866339 B CN106866339 B CN 106866339B
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heat exchanger
tower
natural gas
demethanizer
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CN106866339A (zh
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蒲黎明
周璇
王科
李莹珂
李龙
龙海洋
陈运强
田静
王毅
陆永康
汤晓勇
张雷果
王长锋
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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中回收乙烷联产粗氦的装置及方法，装置包括依次相连的预冷换热器、低温分离器、脱甲烷塔、主换热器、氦气提浓塔、氦气塔顶冷凝器和氦气塔顶回流罐；氦气提浓塔塔底的液相出口依次与主换热器、预冷器换热器、膨胀机连接；氦气提浓塔塔底的液相出口依次与氦气提浓塔塔顶冷凝器、主换热器连接；脱甲烷塔的液相出口与脱乙烷塔相连，脱乙烷塔的气相出口依次与冷剂蒸发器、脱乙烷塔顶回流罐相连；所述预冷换热器与单一冷剂制冷系统相连；所述主换热器与混和冷剂制冷系统相连。本发明在保证外输产品天然气满足国家一类气质标准的天然气高热值要求的前提下，回收乙烷，C3+和氦气，提升天然气经济价值，实现天然气产品多元化。

Description

一种天然气中回收乙烷联产粗氦的装置及方法
技术领域
本发明涉及在天然气中回收乙烷并联产粗氦的装置及方法，特别适用天然气中含有一定量的C2+和少量的氦气的气质条件，达到生产乙烷产品和粗氦的目的。
背景技术
大部分的天然气轻烃回收厂仅回收C3+后将剩余气相作为产品气外输，而天然气中还有大部分的乙烷和一定量的氦气并未回收利用。以乙烷为原料的乙烯工厂建设投资和运行成本均很低，并且氦气(He)因独特的性质而在许多领域有着重要的用途。为更大化的利用产品天然气，实现天然气产品多元化，提升经济价值，将天然气中的乙烷和氦气回收利用不失为一种好的选择。
目前天然气乙烷回收工厂主要采用液相过冷和气相过冷工艺，氦气回收工厂一般是联产LNG，未回收乙烷，缺少一种生产乙烷并联产氦气的有效技术。
发明内容
为了克服现有技术的缺点，本发明提供了一种天然气中回收乙烷联产粗氦的装置及方法，具有原料气适应范围广、乙烷和氦气回收率高和能耗低的优点。
本发明所采用的技术方案是：一种天然气中回收乙烷联产粗氦的装置，包括预冷换热器、低温分离器、脱甲烷塔、脱乙烷塔、主换热器和氦气提浓塔，其中：
预冷换热器、低温分离器、脱甲烷塔、主换热器、氦气提浓塔、氦气塔顶冷凝器和氦气塔顶回流罐依次相连；
氦气提浓塔塔底的液相出口依次与主换热器、预冷器换热器、膨胀机连接；
氦气提浓塔塔底的液相出口依次与氦气提浓塔塔顶冷凝器、主换热器连接；
脱甲烷塔的液相出口与脱乙烷塔相连，脱乙烷塔的气相出口依次与冷剂蒸发器、脱乙烷塔顶回流罐相连；
所述预冷换热器与单一冷剂制冷系统相连；所述主换热器与混和冷剂制冷系统相连。
本发明还提供了一种天然气中回收乙烷联产粗氦的方法，包括如下步骤：含乙烷和氦的干燥天然气进入预冷换热器预冷后，进入低温分离器，然后进入脱甲烷塔；
脱甲烷塔塔底出来的C2+进入脱乙烷塔进行分馏，脱乙烷塔塔顶出来的气相进入冷剂蒸发器冷凝，然后进入脱乙烷塔塔顶回流罐进行分离，得到的气相为乙烷产品；脱乙烷塔底出来的液相为C3+；
脱甲烷塔塔顶出来的气相进入氦气提浓塔，氦气提浓塔塔顶出来的气相进入氦气提浓塔塔顶冷凝器冷凝后，进入氦气提浓塔塔顶回流罐进行分离，分离后得到的气相为粗氦产品；
氦气提浓塔塔底出来的大部分液相依次通过主换热器和预冷器换热器换热后，再通过膨胀机同轴增压端增压后作为产品天然气外输；
氦气提浓塔塔底出来的少部分液相进入氦气提浓塔塔顶冷凝器提供冷量换热后再返输至主换热器中换热回收冷量，提供冷量后的天然气作为燃料气外输。
与现有技术相比，本发明的积极效果是：在保证外输产品天然气满足国家一类气质标准的天然气高热值要求的前提下，回收乙烷，C3+和氦气，提升天然气经济价值，实现天然气产品多元化。并且回收得到的乙烷产品可作为乙烯的优质原料，并且在一定程度少减少了石脑油、原油等其他乙烯原料气的用量，而得到的氦气产品也可用于军工、医疗、科研、石化、医疗、光电子产品的生产，可在很大程度上带动下游产业。
本发明设置两套独立的制冷系统，可以根据原料气不同的气质条件做出相应的调整，因此具有适应范围广的特点。
本发明中乙烷回收率高达90％以上，乙烷混烃回收率高达95％以上，氦气回收率高达99％以上。
附图说明
本发明将通过例子并参照附图的方式说明，其中：
图1是本装置的工艺原理流程图。
具体实施方式
一种天然气中回收乙烷联产粗氦的装置，如图1所示，包括：预冷换热器1、低温分离器2、膨胀机3、脱甲烷塔4、脱甲烷塔塔底重沸器5、脱乙烷塔6、脱乙烷塔塔底重沸器7、冷剂蒸发器8、脱乙烷塔塔顶回流罐9、脱乙烷塔塔顶回流泵10、单一冷剂制冷系统11、主换热器12、氦气提浓塔13、氦气提浓塔塔底蒸发器14、氦气提浓塔塔顶冷凝器15、氦气提浓塔塔顶回流罐16、氦气提浓塔塔顶回流泵17和混合冷剂制冷系统18。其中：
预冷换热器1依次与低温分离器2、膨胀机3、脱甲烷塔4和主换热器12连接；主换热器12的天然气出口与脱甲烷塔4上部进口相连。
低温分离器2出口的液相与脱甲烷塔4直接相连；脱甲烷塔4出口的液相与脱乙烷塔6直接相连；脱乙烷塔6与冷剂蒸发器8、脱乙烷塔顶回流罐9、脱乙烷塔顶回流泵10依次相连；脱乙烷塔顶回流泵10的出口与脱乙烷塔6塔顶入口相连；脱甲烷塔4底部设有脱甲烷塔底重沸器5，用于为脱甲烷塔4底部提供热量；脱乙烷塔6底部设有脱乙烷塔底重沸器7，用于为脱乙烷塔6底部提供热量。
脱甲烷塔4塔顶的气相出口分别与氦气提浓塔塔底蒸发器14和主换热器12相连，主换热器12的天然气出口分别与脱甲烷塔4塔顶的进口和氦气提浓塔13的进口相连。氦气提浓塔塔底蒸发器14的物流出口与氦气提浓塔13的进口相连。氦气提浓塔13与氦气塔顶冷凝器15、氦气塔顶回流罐16、氦气塔顶回流泵17依次相连；氦气提浓塔塔顶回流泵17的出口与氦气提浓塔13塔顶入口相连。氦气提浓塔13底部设有氦气提浓塔塔底蒸发器14，用于为氦气提浓塔13底部提供热量；单一冷剂制冷系统11与预冷换热器1相连，用于为预冷换热器1提供换热所需的冷量；混合冷剂制冷系统18与主换热器12相连，用于为主换热器12提供换热所需的冷量。
氦气提浓塔13塔底的液相出口依次与主换热器12、预冷器换热器1、膨胀机3连接；氦气提浓塔13塔底的液相出口依次与氦气提浓塔塔顶冷凝器15、主换热器12连接。
由于含乙烷和氦的原料天然气的预冷、产品天然气的复热(冷量回收)在预冷换热器1中进行，因此预冷换热器1与单一冷剂制冷系统11相连，为其提供不足的冷量。预冷的原料天然气和脱除C2+的天然气的冷凝，脱出氦气的天然气的复热(冷量回收)均在主换热器12中进行，因此主换热器12与混和冷剂制冷系统18相连，为其提供不足的冷量。
本发明还提供了一种天然气中回收乙烷联产粗氦的方法，包括如下步骤：
3.0～～7.0MPa的干燥含乙烷和氦天然气与预冷换热器1相连，经过预冷换热器1预冷至-40～～-65℃左右后，经过低温分离器2分离出的气相大部分(约60～～70％左右)进入膨胀机3，膨胀后的气相压力至2.0～～4.0MPa后直接进入脱甲烷塔4，剩余少部分气相(约30～～40％左右)继续进入主换热器12进一步冷凝至-70～～-95℃后再进入脱甲烷塔4上部。低温分离器2分离出的液相则节流至2.2～～4.5MPa后直接进入脱甲烷塔4。脱甲烷塔的压力控制在2.8～～3.6MPa。
脱甲烷塔4塔底出来的C2+直接进入脱乙烷塔6，脱乙烷塔6的压力控制在2.6～～3.2MPa，经过脱乙烷塔6分馏后，塔顶出来的气相与冷剂蒸发器8相连，部分冷凝至-30～15℃左右后通过脱乙烷塔塔顶回流罐9分离得到的液体则通过脱乙烷塔塔顶回流泵10输送至脱乙烷塔6塔顶作为其回流液，脱乙烷塔塔顶回流罐9分离得到的气相则为乙烷产品，可直接外售，也可以冷凝为液体外售。
脱甲烷塔4塔顶出来的气相少部分与氦气提浓塔塔底蒸发器14相连，为其提供热量，剩余大部分进入主换热器12，冷凝至-90～～-115℃后，一部分(约10～～20％左右)返回至脱甲烷塔4塔顶，剩余部分与来自氦气提浓塔塔底蒸发器14的物流混合后直接进入氦气提浓塔13，氦气提浓塔压力控制在2.7～～3.3MPa。氦气提浓塔13塔顶出来的-95～～-105℃气相进入氦气提浓塔塔顶冷凝器15，被来自氦气提浓塔13塔底的少部分液相提供冷量冷凝至-130～～-150℃后，进入氦气提浓塔塔顶回流罐16进行分离：分离后得到的液相通过氦气提浓塔塔顶回流泵17直接输送至氦气提浓塔13塔顶，作为其回流液；分离后得到的气相为粗氦产品，经过精氦装置继续处理则可得到精氦产品。
氦气提浓塔13塔底出来的大部分(75～～95％)液相依次通过主换热器12和预冷器换热器1换热至20～～40℃后，再通过膨胀机3同轴增压端增压后作为产品天然气外输。氦气提浓塔13塔底出来的少部分液相经节流至0.2～～0.4MPa后进入氦气提浓塔塔顶冷凝器15提供冷量换热后再返输至主换热器12中换热回收冷量，提供冷量后的天然气输送至工厂燃料气系统作为工厂燃料气，或者增压后外输。
本发明中与预冷换热器和主换热器相连的两个制冷系统为两个不同温位的制冷系统，两者独立，互不干扰，可在一定程度增加装置的稳定性。
本发明中与预冷换热器相连的单一冷剂制冷系统11中的单一冷剂是指常温沸点在-35～～-60℃左右的制冷剂，例如：丙烷、R134a、氨等。
本发明中与预冷换热器相连的混合冷剂制冷系统18中的混合冷剂是指常温沸点在-70～～125℃左右的混合制冷剂，其中主要含有：甲烷、乙烷、乙烯、丙烷、丁烷、戊烷和氮气等。
本发明中脱甲烷塔、脱乙烷塔和氦气提浓塔均分别设有重沸器。
本发明中脱甲烷塔、脱乙烷塔和氦气提浓塔可以是板式塔也可以是填料塔。
本发明中脱乙烷塔底出来的液相为C3+，可根据用户需求决定是否通过脱丁烷塔分馏得到LPG产品和稳定轻烃产品外售，也可以直接外售。实现产品多元化。

Claims (8)

1.一种天然气中回收乙烷联产粗氦的装置，其特征在于：包括预冷换热器、低温分离器、脱甲烷塔、脱乙烷塔、主换热器和氦气提浓塔，其中：
预冷换热器、低温分离器、脱甲烷塔、主换热器、氦气提浓塔、氦气塔顶冷凝器和氦气塔顶回流罐依次相连；
氦气提浓塔塔底的液相出口分成两路，一路依次与主换热器、预冷器换热器、膨胀机连接，另一路依次与氦气提浓塔塔顶冷凝器、主换热器连接；
脱甲烷塔的液相出口与脱乙烷塔相连，脱乙烷塔的气相出口依次与冷剂蒸发器、脱乙烷塔顶回流罐相连；
所述预冷换热器与单一冷剂制冷系统相连；所述主换热器与混和冷剂制冷系统相连；
所述脱甲烷塔和脱乙烷塔底部均设有重沸器，所述氦气提浓塔底部设有蒸发器；
所述脱乙烷塔顶回流罐依次与脱乙烷塔顶回流泵和脱乙烷塔相连。
2.根据权利要求1所述的一种天然气中回收乙烷联产粗氦的装置，其特征在于：所述脱甲烷塔塔顶的气相出口分别与氦气提浓塔塔底蒸发器和主换热器相连，主换热器的天然气出口分别与脱甲烷塔塔顶进口和氦气提浓塔进口相连；氦气提浓塔塔底蒸发器的物流出口与氦气提浓塔进口相连。
3.根据权利要求1所述的一种天然气中回收乙烷联产粗氦的装置，其特征在于：所述氦气塔顶回流罐依次与氦气提浓塔塔顶回流泵和氦气提浓塔相连。
4.根据权利要求1所述的一种天然气中回收乙烷联产粗氦的装置，其特征在于：所述低温分离器的气相出口依次与膨胀机、脱甲烷塔相连；所述低温分离器的气相出口依次与主换热器和脱甲烷塔相连；所述低温分离器的液相出口与脱甲烷塔相连。
5.一种天然气中回收乙烷联产粗氦的方法，其特征在于：包括如下步骤：含乙烷和氦的干燥天然气进入预冷换热器预冷后，进入低温分离器，然后进入脱甲烷塔；
脱甲烷塔塔底出来的C2+进入脱乙烷塔进行分馏，脱乙烷塔塔顶出来的气相进入冷剂蒸发器冷凝，然后进入脱乙烷塔塔顶回流罐进行分离，得到的气相为乙烷产品；脱乙烷塔底出来的液相为C3+；
脱甲烷塔塔顶出来的气相进入氦气提浓塔，氦气提浓塔塔顶出来的气相进入氦气提浓塔塔顶冷凝器冷凝后，进入氦气提浓塔塔顶回流罐进行分离，分离后得到的气相为粗氦产品；
氦气提浓塔塔底出来的液相分成两路：其中，大部分液相依次通过主换热器和预冷器换热器换热后，再通过膨胀机同轴增压端增压后作为产品天然气外输；少部分液相进入氦气提浓塔塔顶冷凝器提供冷量换热后再返输至主换热器中换热回收冷量，提供冷量后的天然气作为燃料气外输。
6.根据权利要求5所述的一种天然气中回收乙烷联产粗氦的方法，其特征在于：所述低温分离器分离出的大部分气相进入膨胀机，膨胀后的气相进入脱甲烷塔；剩余气相进入主换热器冷凝后进入脱甲烷塔。
7.根据权利要求5所述的一种天然气中回收乙烷联产粗氦的方法，其特征在于：所述脱乙烷塔塔顶回流罐分离后得到的液相通过脱乙烷塔塔顶回流泵输送至脱乙烷塔塔顶作为回流液；所述氦气提浓塔塔顶回流罐分离后得到的液相通过氦气提浓塔塔顶回流泵输送至氦气提浓塔塔顶作为回流液。
8.根据权利要求5所述的一种天然气中回收乙烷联产粗氦的方法，其特征在于：所述脱甲烷塔塔顶出来的气相少部分进入氦气提浓塔塔底蒸发器，为
其提供热量，剩余大部分进入主换热器冷凝后，一部分返回至脱甲烷塔塔顶，
剩余部分与来自氦气提浓塔塔底蒸发器的物流混合后进入氦气提浓塔。
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