CN109028758A - 一种采用混合冷剂制冷的天然气乙烷回收装置及方法 - Google Patents

一种采用混合冷剂制冷的天然气乙烷回收装置及方法 Download PDF

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CN109028758A
CN109028758A CN201810889521.5A CN201810889521A CN109028758A CN 109028758 A CN109028758 A CN 109028758A CN 201810889521 A CN201810889521 A CN 201810889521A CN 109028758 A CN109028758 A CN 109028758A
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azeotrope
ice chest
natural gas
domethanizing column
gas
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周璇
王科
蒲黎明
涂洁
陈运强
郭建
张庆林
刘玉洁
田静
杜娟
胡益武
李莹珂
汤晓勇
李娜
郭成华
汪贵
龙海洋
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
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    • F25J2200/00—Processes or apparatus using separation by rectification
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Abstract

本发明公开了一种采用混合冷剂制冷的天然气乙烷回收装置及方法，装置包括冷箱和分别与冷箱连接的低温分离器、混合冷剂压缩机、脱甲烷塔和脱乙烷塔，其中：所述低温分离器出口的液相与脱甲烷塔直接相连；脱甲烷塔出口的液相与脱乙烷塔直接相连；低温分离器出口的气相分成两股，一股通过J‑T阀或膨胀机进入脱甲烷塔，另一股经冷箱进入脱甲烷塔上部；冷箱的气相冷剂出口依次与混合冷剂压缩机、混合冷剂冷凝器连接，混合冷剂冷凝器的出口依次与冷箱、混合冷剂J‑T阀、冷箱、混合冷剂压缩机连接。本发明针对乙烷回收工厂处理规模不大，原料气压力小于5MPa，外输压力不高的情况，既具有较高的乙烷回收率，又有节省投资和降低能耗的优点。

Description

一种采用混合冷剂制冷的天然气乙烷回收装置及方法
技术领域
本发明涉及轻烃回收领域，尤其是乙烷回收领域，具体为一种采用混合冷剂制冷在天然气回收乙烷的工艺装置及方法，针对乙烷回收工厂处理规模不大，原料气压力小于5MPa，外输压力不高的情况，既具有较高的乙烷回收率，又有节省投资和降低能耗的优点。
背景技术
2016年，中国乙烯产能达到了2269万吨，仅次于美国位于第二位。2016年，我国乙烯平均装置开工率达到了96％，产量已经达到了2170万吨。同期，我国乙烯表观消费量达到了2336万吨，当量消费量达到了3940万吨。按照当量消费量来看，2016年我国乙烯自给率提高到了55％，但是缺口仍然巨大。
乙烷制乙烯具备“一高三低”的优势，即烯烃收率高、工厂相对投资低、生产成本低、能耗低，生产乙烷产品需求愈发强烈。乙烷目前大量存在于产品天然气中，利用率较低，为更高效地利用天然气，实现天然气产品多元化，大力发展乙烷回收技术具有重要意义。
目前天然气乙烷回收工厂主要多数采用“丙烷/丙烯预冷+膨胀机制冷”工艺。因为采用单组分制冷剂预冷，原料气预冷温度较低，主要依靠膨胀制冷提供冷量，当原料气压力不太高，不能提供足够的冷量时，乙烷收率则相对较低，不够经济。虽然“阶式制冷+膨胀机制冷工艺”可以解决能耗大，操作复杂的问题。但是针对小规模的乙烷回收工厂，“混合冷剂制冷工艺”具有投资省，能耗低，操作简单，乙烷收率高的特点。
发明内容
为了克服现有技术的缺点，本发明提供了一种采用混合冷剂制冷的天然气乙烷回收装置及方法，对于生产规模不大的工厂，针对原料气压力不高，产品气外输压力要求不高，原料气和产品天然气的压力能很小的情况，具有投资省、能耗低和操作简单灵活的优点。
本发明所采用的技术方案是：一种采用混合冷剂制冷的天然气乙烷回收装置，包括冷箱和分别与冷箱连接的低温分离器、混合冷剂压缩机、脱甲烷塔和脱乙烷塔，其中：所述低温分离器出口的液相与脱甲烷塔直接相连；脱甲烷塔出口的液相与脱乙烷塔直接相连；低温分离器出口的气相分成两股，一股通过J-T阀或膨胀机进入脱甲烷塔，另一股经冷箱进入脱甲烷塔上部；冷箱的气相冷剂出口依次与混合冷剂压缩机、混合冷剂冷凝器连接，混合冷剂冷凝器的出口依次与冷箱、混合冷剂J-T阀、冷箱、混合冷剂压缩机连接。
本发明还提供了一种采用混合冷剂制冷的天然气乙烷回收方法，包括如下内容：
一、精馏：
1.7～～5.0MPa.g的干燥含乙烷天然气经过冷箱预冷至-75～～-90℃后进入低温分离器进行气液分离：分离出的气相大部分通过J-T阀节流至1.0～～3.5MPa.g后进入脱甲烷塔，少部分气相进入冷箱冷凝至-80～～-110℃成液体后进入脱甲烷塔上部；分离出的液相节流至1.0～～3.5MPa.g后进入脱甲烷塔，脱甲烷塔的压力控制在1.0～～3.4MPa.g；脱甲烷塔塔底出来的C2+进入脱乙烷塔，脱乙烷塔的压力控制在0.8～～3.2MPa.g，经过脱乙烷塔分馏后，塔顶出来的气相经冷箱冷凝至-20～5℃后进入脱乙烷塔塔顶回流罐进行气液分离：分离出的液体送至脱乙烷塔塔顶作为回流液，分离得到的气相则为乙烷产品。
二、混合冷剂制冷：
从冷箱出来的0～40℃、0.1～0.6MPa.g的气相冷剂进入混合冷剂压缩机增压为80～130℃、1.5～3.5MPa.g后进入混合冷剂冷凝器冷凝为20～50℃，再进入冷箱冷凝为-70～-100℃，然后进入混合冷剂节流阀节流为-90～-120℃，最后经冷箱复热后进入混合冷剂压缩机完成制冷循环。
与现有技术相比，本发明的积极效果是：
当原料气压力不高，产品气外输压力要求不高，原料气和产品天然气的压力能很小时，采用混合冷剂制冷，可以在保证有较高的乙烷收率前提下，避免产品气进一步增压，同时可以取消干气回流压缩机。针对这种乙烷回收工厂处理规模不大，尤其是针对原料气压力小于5MPa的乙烷回收工厂，乙烷回收装置可利用压力能很小，具有装置简单，采购容易，混合冷剂压缩机功率较低，降低投资、能耗低和操作简单灵活的优点。
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是本装置实施例1的工艺原理流程图；
图2是本装置实施例2的工艺原理流程图；
图3是本装置实施例3的工艺原理流程图。
具体实施方式
实例1：
一种采用混合冷剂制冷的天然气乙烷回收装置，如图1所示，包括：冷箱1、低温分离器2、混合冷剂压缩机3、J-T阀4、脱甲烷塔5、脱甲烷塔塔底重沸器6、脱乙烷塔7、脱乙烷塔塔顶回流罐8、脱乙烷塔塔顶回流泵9、脱乙烷塔塔底重沸器10、混合冷剂冷凝器11、混合冷剂J-T阀12。
冷箱1是乙烷回收装置原料气预冷和低温气过冷的场所，冷箱1分别与低温分离器2、混合冷剂制冷系统3和脱甲烷塔5和脱乙烷塔7连接。
低温分离器2出口的液相与脱甲烷塔5直接相连；脱甲烷塔5出口的液相与脱乙烷塔7直接相连；脱乙烷塔7与冷箱1、脱乙烷塔顶回流罐8、脱乙烷塔顶回流泵9依次相连；脱乙烷塔顶回流泵9的出口与脱乙烷塔7塔顶入口相连；脱甲烷塔5底部设有脱甲烷塔底重沸器6，用于为脱甲烷塔5底部提供热量；脱乙烷塔7底部设有脱乙烷塔底重沸器10，用于为脱乙烷塔7底部提供热量。
低温分离器2出口的气相分成两股，一股通过J-T阀4进入脱甲烷塔5，另一股经冷箱1进入脱甲烷塔5上部。
脱甲烷塔5塔顶出来的气相通过冷箱1后外输。
冷箱1的气相冷剂出口依次与混合冷剂压缩机、混合冷剂冷凝器11连接，混合冷剂冷凝器11的出口依次与冷箱1、混合冷剂J-T阀12、冷箱1、混合冷剂压缩机3连接，形成制冷循环。
本发明还提供了一种采用混合冷剂制冷的天然气乙烷回收方法，包括如下步骤：
一、精馏系统：
1.7～～5.0MPa.g的干燥含乙烷天然气与冷箱1相连，经过冷箱1预冷至-75～～-90℃左右后，经过低温分离器2分离出的气相大部分(约60～～90mol％左右)通过J-T阀4，节流至1.0～～3.5MPa.g后直接进入脱甲烷塔5，剩余少部分(约10～～40mol％左右)气相继续进入冷箱1进一步冷凝至-80～～-110℃成液体后再进入脱甲烷塔5上部。低温分离器2分离出的液相则节流至1.0～～3.5MPa.g后直接进入脱甲烷塔5。脱甲烷塔的压力控制在1.0～～3.4MPa.g。
脱甲烷塔5塔底出来的C2+直接进入脱乙烷塔7，脱乙烷塔7的压力控制在0.8～～3.2MPa.g，经过脱乙烷塔7分馏后，塔顶出来的气相与冷箱1相连，部分冷凝至-20～5℃左右后通过脱乙烷塔塔顶回流罐8分离得到的液体则通过脱乙烷塔塔顶回流泵9输送至脱乙烷塔7塔顶作为其回流液，脱乙烷塔塔顶回流罐8分离得到的气相则为乙烷产品。
脱甲烷塔5塔顶出来的气相通过冷箱1复热后直接外输。
二、制冷系统：
由混合冷剂压缩机3和混合冷剂冷凝器11组成，主要是为冷箱1换热提供不足的冷量。从冷箱1出来的气相冷剂(0～40℃，0.1～0.6MPa.g)进入混合冷剂压缩机3，增压后(80～130℃，1.5～3.5MPa.g)进入混合冷剂冷凝器11部分冷凝后(20～50℃)进入冷箱1全部冷凝后(-70～-100℃)，进入混合冷剂节流阀12节流后(-90～-120℃)提供高品位的冷量，进入冷箱1复热后进入混合冷剂压缩机3完成制冷循环。
混合冷剂制冷可以由甲烷(20～40mol％)、乙烷(10～35mol％)、乙烯(10～35mol％)、丙烷(10～45mol％)、丁烷(5～35mol％)、戊烷(5～35mol％)和氮气(5～35mol％)中的一种或者几种组成。
实例2：
制冷系统与实例1一致。当原料气有较小的压力能可利用时，可以将J-T阀改为膨胀机，获得较高的制冷效率，同时外输产品气可回收部分压力能，在同等收率的前提下，降低装置能耗。
实例3：
冷箱、脱甲烷塔、脱乙烷塔装置及工艺流程均与实例1一致。由于外输管网背压较高，脱甲烷塔5塔顶出来的气相通过冷箱1复热不能直接外输，因此需经过产品气压缩机13增压并经产品气冷却器14冷却后外输。

Claims (10)

1.一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：包括冷箱和分别与冷箱连接的低温分离器、混合冷剂压缩机、脱甲烷塔和脱乙烷塔，其中：所述低温分离器出口的液相与脱甲烷塔直接相连；脱甲烷塔出口的液相与脱乙烷塔直接相连；低温分离器出口的气相分成两股，一股通过J-T阀或膨胀机进入脱甲烷塔，另一股经冷箱进入脱甲烷塔上部；冷箱的气相冷剂出口依次与混合冷剂压缩机、混合冷剂冷凝器连接，混合冷剂冷凝器的出口依次与冷箱、混合冷剂J-T阀、冷箱、混合冷剂压缩机连接。
2.根据权利要求1所述的一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：脱甲烷塔的气相出口经过冷箱后接入产品天然气外输管道。
3.根据权利要求1所述的一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：脱甲烷塔的气相出口依次与冷箱、产品气压缩机、产品气冷却器和产品天然气外输管道连接。
4.根据权利要求1所述的一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：脱乙烷塔与冷箱、脱乙烷塔顶回流罐、脱乙烷塔顶回流泵依次相连；脱乙烷塔顶回流泵的出口与脱乙烷塔塔顶入口相连。
5.根据权利要求1所述的一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：脱甲烷塔底部设有脱甲烷塔底重沸器。
6.根据权利要求1所述的一种采用混合冷剂制冷的天然气乙烷回收装置，其特征在于：脱乙烷塔底部设有脱乙烷塔底重沸器。
7.一种采用混合冷剂制冷的天然气乙烷回收方法，其特征在于：包括如下内容：
一、精馏：
1.7～～5.0MPa.g的干燥含乙烷天然气经过冷箱预冷至-75～～-90℃后进入低温分离器进行气液分离：分离出的气相大部分通过J-T阀节流至1.0～～3.5MPa.g后进入脱甲烷塔，少部分气相进入冷箱冷凝至-80～～-110℃成液体后进入脱甲烷塔上部；分离出的液相节流至1.0～～3.5MPa.g后进入脱甲烷塔，脱甲烷塔的压力控制在1.0～～3.4MPa.g；脱甲烷塔塔底出来的C2+进入脱乙烷塔，脱乙烷塔的压力控制在0.8～～3.2MPa.g，经过脱乙烷塔分馏后，塔顶出来的气相经冷箱冷凝至-20～5℃后进入脱乙烷塔塔顶回流罐进行气液分离：分离出的液体送至脱乙烷塔塔顶作为回流液，分离得到的气相则为乙烷产品。
二、混合冷剂制冷：
从冷箱出来的0～40℃、0.1～0.6MPa.g的气相冷剂进入混合冷剂压缩机增压为80～130℃、1.5～3.5MPa.g后进入混合冷剂冷凝器冷凝为20～50℃，再进入冷箱冷凝为-70～-100℃，然后进入混合冷剂节流阀节流为-90～-120℃，最后经冷箱复热后进入混合冷剂压缩机完成制冷循环。
8.根据权利要求7所述的一种采用混合冷剂制冷的天然气乙烷回收方法，其特征在于：脱甲烷塔塔顶出来的气相通过冷箱复热后直接作为产品天然气外输。
9.根据权利要求7所述的一种采用混合冷剂制冷的天然气乙烷回收方法，其特征在于：脱甲烷塔塔顶出来的气相通过冷箱复热后，再经过产品气压缩机增压，最后经产品气冷却器冷却后作为产品天然气外输。
10.根据权利要求7所述的一种采用混合冷剂制冷的天然气乙烷回收方法，其特征在于：所述混合冷剂由甲烷、乙烷、乙烯、丙烷、丁烷、戊烷和氮气中的一种或者几种组成。
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