CN103409188B - 一种天然气液化过程中脱除重烃的工艺装置及方法 - Google Patents

一种天然气液化过程中脱除重烃的工艺装置及方法 Download PDF

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CN103409188B
CN103409188B CN201310335521.8A CN201310335521A CN103409188B CN 103409188 B CN103409188 B CN 103409188B CN 201310335521 A CN201310335521 A CN 201310335521A CN 103409188 B CN103409188 B CN 103409188B
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王科
刘家洪
蒲黎明
黄勇
陆永康
陈运强
冼祥发
李莹珂
谌天兵
韩淑怡
宋德琦
郭成华
法玉晓
王刚
姜宁
龙海洋
田静
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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液化过程中脱除重烃的工艺装置及方法，工艺装置包括依次连接的预冷器、烃液分离器、膨胀机、脱重烃塔、第二节流阀、脱烃冷箱和脱乙烷塔。本发明的积极效果是：利用天然气自身压力经膨胀机膨胀降温，与节流阀相比得到天然气温度更低，膨胀机可以与压缩机或发电机连接来回收部分能量，实现节能；利用乙烷换热器与脱烃冷箱实现装置内能量的充分交换，避免了外加冷源，减少了投资、实现了节能降耗；本工艺重烃脱除效果好，将天然气中的重烃组分尽可能地脱除，有利于后续液化工艺，有效避免重烃冻堵，满足了天然气液化的需要。

Description

一种天然气液化过程中脱除重烃的工艺装置及方法
技术领域
本发明涉及一种在天然气液化过程中天然气经预冷后利用自身压力膨胀制冷脱除重烃的工艺装置及方法，特别针对用于大型天然气液化过程中脱除重烃的工艺装置及方法。
背景技术
天然气在液化之前都必须经过深度预处理，其中包括脱除所含的重烃组分，从而有效避免天然气在液化过程中杂质引起冻堵，尤其是重烃组分在低温环境下冷凝、冻结而堵塞管道、阀门和板翅式换热器等设备。国内外已有的天然气脱除重烃方法主要有精馏法及吸附法，这两种方法中天然气均是在外加冷源的条件下，采用精馏或吸附的方法脱除重烃后进入天然气液化的下一步工序。
目前天然气液化工艺大致可分为阶式制冷循环、混合冷剂循环和膨胀循环三种方式，这三种制冷工艺中高压天然气从气态冷凝至液态至-135~-155℃后节流降压至常压储存。高压天然气内蕴含着巨大的压力能，再通过调压设备调压的过程中，这部分压力能往往被白白的浪费掉，另外，由于天然气急剧降压、降温对调压设备及管道设备的要求也很高。如果将这部分压力能加以利用，可以实现节能降耗的目的。
因此，设计一种利用天然气压力能脱除天然气中含有的重烃组分势在必行。
发明内容
为了克服现有技术的上述缺点，本发明提供了在天然气液化过程中一种采用膨胀机脱除天然气中重烃的工艺装置及方法，具有能耗低、回收部分冷量等特征。
本发明解决其技术问题所采用的技术方案是：一种天然气液化过程中脱除重烃的工艺装置，包括依次连接的预冷器、烃液分离器、膨胀机、脱重烃塔、第二节流阀、脱烃冷箱和脱乙烷塔；所述烃液分离器的底部出口依次与第一节流阀、脱烃冷箱和脱重烃塔中部进口连接；所述脱重烃塔的顶部出口依次与脱重烃塔冷凝器、脱重烃塔回流罐、脱重烃塔回流泵和脱重烃塔的上部进口连接；所述脱乙烷塔的顶部出口依次与脱烃冷箱、脱乙烷塔回流罐、脱乙烷塔回流泵和脱乙烷塔的上部进口连接；脱乙烷塔回流罐的顶部出口与乙烷气换热器的壳程进口连接；乙烷气换热器的管程出口依次与脱烃冷箱、第三节流阀和脱重烃塔的中部进口连接。
本发明还公开了一种天然气液化过程中脱除重烃的工艺方法，包括如下步骤：
第一步、将经脱硫、脱碳、脱水后的含重烃天然气分为两股物流：一股物流经预冷器冷却后，进入烃液分离器进行气液分离，其中：气相经膨胀机膨胀后进入脱重烃塔进行精馏；液相经第一节流阀节流降压后，进入脱烃冷箱冷却降温；另一股物流进入乙烷气换热器，与来自脱乙烷塔回流罐的气相换热后，进入脱烃冷箱降温，然后经第三节流阀节流降压；
第二步、将经脱烃冷箱冷却降温，以及经第三节流阀节流降压后的两股物流混合，从脱重烃塔中部进口进入脱重烃塔进行精馏，经过精馏，天然气中的大部分重烃被脱除后从塔顶排出；
第三步、将从脱重烃塔顶部排出的天然气送入脱重烃塔冷凝器降温，然后进入脱重烃塔回流罐中进行气液分离，分离后的气相进入天然气液化的下一步工序；分离后的液相进入脱重烃塔回流泵，经增压后进入脱重烃塔的上部；
第四步、将脱重烃塔底部的液体送入第二节流阀节流降压后送入脱烃冷箱中换热升温，然后进入脱乙烷塔中精馏；
第五步、将脱乙烷塔的塔顶气送入脱烃冷箱降温，然后进入脱乙烷塔回流罐进行气液分离：分离后的气相进入乙烷气换热器中换热升温，然后通过送入工厂燃料气系统，分离后的液相进入脱乙烷塔回流泵增压后送入到脱乙烷塔的顶部；
第六步、将脱乙烷塔底部的脱乙烷油通过管道送入下一步工序处理。
与现有技术相比，本发明的积极效果是：利用天然气自身压力经膨胀机膨胀降温，与节流阀相比得到天然气温度更低，膨胀机可以与压缩机或发电机连接来回收部分能量，实现节能；利用乙烷换热器与脱烃冷箱实现装置内能量的充分交换，避免了外加冷源，减少了投资、实现了节能降耗；本工艺重烃脱除效果好，将天然气中的重烃组分尽可能地脱除，有利于后续液化工艺，有效避免重烃冻堵，满足了天然气液化的需要。
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是本发明的系统原理示意图。
具体实施方式
一种天然气液化过程中脱除重烃的工艺装置，如图1所示。
图中：1、管道；2、管道；3、预冷器；4、管道；5、烃液分离器；6、管道；7、管道；8、第一节流阀；9、管道；10、膨胀机；11、管道；12、脱重烃塔；13、管道；14、脱重烃塔冷凝器；15、管道；16、脱重烃塔回流罐；17、管道；18、管道；19、脱重烃塔回流泵；20、管道；21、管道；22、管道；23、第二节流阀；24、管道；25、脱烃冷箱26、管道；27、管道；28、管道；29、第三节流阀；30、管道；31、脱乙烷塔；32、管道；33、管道；34、脱乙烷塔回流罐；35、管道；36、管道；37、脱乙烷塔回流泵；38、管道；39、管道；40、管道；41、乙烷气换热器；42、管道；43、管道；44、发电机。其中：
预冷器3依次与烃液分离器5、膨胀机10、脱重烃塔12、第二节流阀23、脱烃冷箱25和脱乙烷塔31连接；烃液分离器5底部出口依次与第一节流阀8、脱烃冷箱25和脱重烃塔12中部进口连接；膨胀机10与发电机44连接；脱重烃塔12顶部出口依次与脱重烃塔冷凝器14、脱重烃塔回流罐16、脱重烃塔回流泵19和脱重烃塔12上部进口连接；脱乙烷塔31顶部出口依次与脱烃冷箱25、脱乙烷塔回流罐34、脱乙烷塔回流泵37和脱乙烷塔31上部进口连接；脱乙烷塔回流罐34顶部出口与乙烷气换热器41壳程进口连接；乙烷气换热器41管程出口依次与脱烃冷箱25、第三节流阀29和脱重烃塔12中部进口连接。
所述膨胀机10可以采用透平技术与发电机44连接，也可以采用透平技术与压缩机连接。所述脱重烃塔12可以是板式塔也可以是填料塔。
本发明还提供了一种天然气液化过程中脱除重烃的工艺方法，包括如下步骤：
第一步、将来自管道1的经脱硫、脱碳、脱水后的含重烃天然气分为两股物流：一股物流经管道2进入预冷器3冷却至-40~-35℃进入烃液分离器5进行气液分离，其中：经过气液分离后的天然气气相经管道6进入膨胀机10至3000kPa~5500kPa膨胀后经管道11从脱重烃塔12下部进口进入脱重烃塔12进行精馏；经过气液分离后的液相（烃液）经管道7去第一节流阀8节流降压至3000kPa~5500kPa后，经管道9进入脱烃冷箱25冷却降温至-70~-55℃后，进入管道27；另一股物流经管道40进入乙烷气换热器41内，与来自脱乙烷塔回流罐34的气相换热后，经管道43进入脱烃冷箱25降温至-40~-35℃，再经管道28去第三节流阀29节流降压至3000kPa~5500 kPa后进入管道30；
第二步、将来自管道27和管道30的两股物流混合，通过管道21从脱重烃塔12中部进口进入脱重烃塔12进行精馏，经过精馏，天然气中的大部分重烃被脱除后从塔顶排出；此处之采用“大部分”而非精确的某一比例，是由于受到原料气组成、精馏塔的操作条件等许多因素，无法指定“大部分”是什么比例，脱重烃的最终目的是避免重烃冻堵设备和管道，只要天然气中重烃的含量在后面天然气液化的工序中无冻堵现象就满足条件。
第三步、将从脱重烃塔12顶部出来的天然气通过管道13进入脱重烃塔冷凝器14降温至-65~-80℃，通过管道15进入脱重烃塔回流罐16中进行气液分离，分离后的气相（即脱除了重烃的干天然气）通过管道17进入天然气液化的下一步工序；分离后的液相通过管道18进入到脱重烃塔回流泵19，经增压至4000kPa~6000 kPa后通过管道20送入到脱重烃塔12的上部；
第四步、将脱重烃塔12底部的液体通过管道22进入第二节流阀23节流降压至1000kPa~2500 kPa后通过管道24送入脱烃冷箱25中换热升温，然后通过管道26进入到脱乙烷塔31中精馏；
第五步、将脱乙烷塔31的塔顶气通过管道32进入脱烃冷箱25降温至-45~-20℃，通过管道33进入脱乙烷塔回流罐34进行气液分离：气液分离后的气相通过管道35进入到乙烷气换热器41中换热升温至0~25℃，然后通过管道42送入工厂燃料气系统，气液分离后的液相通过管道36进入到脱乙烷塔回流泵37增压至1500kPa~3000 kPa后通过管道38送入到脱乙烷塔31的顶部；
第六步、将脱乙烷塔31底部的脱乙烷油通过管道39送入下一步工序处理。

Claims (2)

1.一种天然气液化过程中脱除重烃的工艺装置，其特征在于：包括依次连接的预冷器、烃液分离器、膨胀机、脱重烃塔、第二节流阀、脱烃冷箱和脱乙烷塔；所述烃液分离器的底部出口依次与第一节流阀、脱烃冷箱和脱重烃塔中部进口连接；所述脱重烃塔的顶部出口依次与脱重烃塔冷凝器、脱重烃塔回流罐、脱重烃塔回流泵和脱重烃塔的上部进口连接；所述脱乙烷塔的顶部出口依次与脱烃冷箱、脱乙烷塔回流罐、脱乙烷塔回流泵和脱乙烷塔的上部进口连接；脱乙烷塔回流罐的顶部出口与乙烷气换热器的壳程进口连接；乙烷气换热器的管程出口依次与脱烃冷箱、第三节流阀和脱重烃塔的中部进口连接；所述脱重烃塔为板式塔或填料塔；所述膨胀机与发电机或压缩机连接。
2.一种天然气液化过程中脱除重烃的工艺方法，其特征在于：包括如下步骤：
第一步、将经脱硫、脱碳、脱水后的含重烃天然气分为两股物流：一股物流经预冷器冷却后，进入烃液分离器进行气液分离，其中：气相经膨胀机膨胀后进入脱重烃塔进行精馏；液相经第一节流阀节流降压后，进入脱烃冷箱冷却降温；另一股物流进入乙烷气换热器，与来自脱乙烷塔回流罐的气相换热后，进入脱烃冷箱降温，然后经第三节流阀节流降压；
第二步、将经脱烃冷箱冷却降温，以及经第三节流阀节流降压后的两股物流混合，从脱重烃塔中部进口进入脱重烃塔进行精馏，经过精馏，天然气中的大部分重烃被脱除后从塔顶排出；
第三步、将从脱重烃塔顶部排出的天然气送入脱重烃塔冷凝器降温，然后进入脱重烃塔回流罐中进行气液分离，分离后的气相进入天然气液化的下一步工序；分离后的液相进入脱重烃塔回流泵，经增压后进入脱重烃塔的上部；
第四步、将脱重烃塔底部的液体送入第二节流阀节流降压后送入脱烃冷箱中换热升温，然后进入脱乙烷塔中精馏；
第五步、将脱乙烷塔的塔顶气送入脱烃冷箱降温，然后进入脱乙烷塔回流罐进行气液分离：分离后的气相进入乙烷气换热器中换热升温，然后通过送入工厂燃料气系统，分离后的液相进入脱乙烷塔回流泵增压后送入到脱乙烷塔的顶部；
第六步、将脱乙烷塔底部的脱乙烷油通过管道送入下一步工序处理。
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