CN107098788B - 一种在管道天然气中回收乙烷脱二氧化碳的装置及方法 - Google Patents

一种在管道天然气中回收乙烷脱二氧化碳的装置及方法 Download PDF

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CN107098788B
CN107098788B CN201710418571.0A CN201710418571A CN107098788B CN 107098788 B CN107098788 B CN 107098788B CN 201710418571 A CN201710418571 A CN 201710418571A CN 107098788 B CN107098788 B CN 107098788B
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natural gas
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CN107098788A (zh
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周璇
蒲黎明
王科
李莹珂
王长锋
龙海洋
陈运强
田静
陆永康
王刚
张雷果
王毅
蒋志明
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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
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Abstract

本发明公开了一种在管道天然气中回收乙烷脱二氧化碳的装置及方法，装置包括两个脱水脱碳塔、主换热器和脱甲烷塔，其中：两个脱水脱碳塔的顶部进口均与原料天然气管道连接，两个脱水脱碳塔的底部出口均与主换热器连接；所述主换热器与低温分离器连接，所述低温分离器的气相出口依次与膨胀机、脱甲烷塔连接，所述低温分离器的液相出口与脱甲烷塔中部连接；所述脱甲烷塔的顶部出口依次与主换热器、膨胀机相连；两个脱水脱碳塔的底部进口均与膨胀机出口连接；两个脱水脱碳塔的顶部出口均与再生气压缩机连接。本发明可直接利用吸附剂对CO2的吸附性，在一定程度上脱除CO2，避免在乙烷回收装置脱甲烷塔冻堵，具有投资省和能耗低等优点。

Description

一种在管道天然气中回收乙烷脱二氧化碳的装置及方法
技术领域
本发明涉及在管道天然气中回收乙烷脱CO2的工艺装置及方法，特别适用乙烷回收工厂的原料气为管输天然气，CO2含量为1.5％～2％的气质条件，达到既避免乙烷回收装置冻堵，又能节省投资的目的。
背景技术
近年来，天然气需求量增速明显下降，为实现由注重发展规模和发展速度向注重发展质量和发展效益的重要转型，实现天然气产品的多元化。落实天然气提质提效的发展战略。商品天然气中含有大量的乙烷，而该部分天然气目前作为商品天然气直接输送至用户，而未加以利用，因此避免上游资源的浪费，将天然气的价值最大化，将管输天然气中乙烷回收利用成为一种趋势。
现有的乙烷回收技术均采用了低温分离的方法，如果原料气中的CO2含量较高(GB17820-2012<天然气>中规定一类产品天然气CO2≤2％)，前端不设脱碳装置，乙烷回收装置的脱甲烷塔极易冻堵。而现有的脱CO2方法大多采用湿法脱碳，再采用吸附法脱水，然后再进行乙烷回收。该方法可以从根本上解决CO2冻堵的问题，但是一次性投资和能耗均较高。
发明内容
为了克服现有技术的缺点，本发明提供了一种在管道天然气中回收乙烷脱CO2的回收装置及方法，具有投资省、能耗低和操作灵活的优点。
本发明所采用的技术方案是：一种在管道天然气中回收乙烷脱二氧化碳的装置，包括两个脱水脱碳塔、主换热器和脱甲烷塔，其中：两个脱水脱碳塔的顶部进口均与原料天然气管道连接，两个脱水脱碳塔的底部出口均与主换热器连接；所述主换热器与低温分离器连接，所述低温分离器的气相出口依次与膨胀机、脱甲烷塔连接，所述低温分离器的液相出口与脱甲烷塔中部连接；所述脱甲烷塔的顶部出口依次与主换热器、膨胀机相连；两个脱水脱碳塔的底部进口均与膨胀机出口连接；两个脱水脱碳塔的顶部出口均与再生气压缩机连接。
本发明还提供了一种在管道天然气中回收乙烷脱二氧化碳的方法，包括如下内容：3.0～7.0MPa的原料天然气与脱水脱碳塔A相连，经过脱水脱碳塔A脱水和脱除部分CO2后的干净化气进入主换热器预冷至-40～-65℃，然后进入低温分离器进行气液分离，其中：分离出的气相进入膨胀机，膨胀后的气相压力至2.0～4.0MPa后直接进入脱甲烷塔上部；分离出的液相经节流至2.2～4.5MPa后进入脱甲烷塔中部；脱甲烷塔底部的C2+进入后续工序回收乙烷；脱甲烷塔顶部的产品天然气经过主换热器回收热量后与膨胀机相连，经过膨胀机同轴增压端增压后的产品气大部分外输，小部分进入脱水脱碳塔B，使脱水脱碳塔B再生，然后进入再生气压缩机增压至产品气外输需要的压力后与大部分的产品气汇合后一起外输；脱水脱碳塔A和B在一个周期内，一个塔吸附，另一个塔再生，进入下一个周期后，二者互换，运行期间保持一塔吸附和一塔再生。
与现有技术相比，本发明的积极效果是：针对乙烷回收工厂原料气中CO2含量为1.5％～2％的气质情况的乙烷回收工厂，本发明可直接利用吸附剂对CO2的吸附性，在一定程度上脱除CO2，避免在乙烷回收装置脱甲烷塔冻堵。具有投资省和能耗低等优点。
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是本装置的工艺原理流程图。
具体实施方式
一种在管道天然气中回收乙烷脱CO2的装置，如图1所示，包括：脱水脱碳塔1A&1B、再生气压缩机2、主换热器3、制冷系统4、低温分离器5、膨胀机6、脱甲烷塔7、脱甲烷塔底重沸器8和产品气压缩机9。其中：
脱水脱碳塔1A&1B为原料气脱除水和部分CO2的场所，脱水脱碳塔1A&1B与原料天然气连接；脱水脱碳塔1A&1B还和膨胀机6出口的产品天然气连接；脱水脱碳塔1A&1B出口的干净化气与主换热器3连接；脱甲烷塔7的顶部产品天然气依次与主换热器3、膨胀机6连接，制冷系统4和主换热器3连接，脱甲烷塔7还和脱甲烷塔底重沸器8连接。
来自管道的原料天然气与脱水脱碳塔1A相连，经过脱水脱碳塔1A脱水和脱碳后的干净化气直接进入主换热器3预冷，预冷后的干净化气与低温分离器5相连，低温分离器分离的气相与膨胀机6相连，膨胀降温后的气相直接进入脱甲烷塔7顶部，低温分离器5分离的液相直接与脱甲烷塔7中部相连，脱甲烷塔底部的C2+则进入后续工序回收乙烷。脱甲烷塔顶部的产品天然气经过主换热器3回收热量后与膨胀机6相连，增压后的产品气大部分进入产品气压缩机9增压至需要的外输压力，剩余小部分进入脱水脱碳塔1B，使脱水脱碳塔1B再生，该部分气含有CO2和水，与再生气压缩机2相连，增压后与产品气压缩机9增压后的产品气汇合一起外输。在乙烷回收过程中不足的冷量由制冷系统4提供。
本发明还提供了一种在管道天然气中回收乙烷脱CO2的方法。包括如下步骤：
装置以两塔流程，吸附时间为12小时为例，脱水脱碳塔1A在1个操作周期内吸附12小时，脱水脱碳塔1B热吹6小时，冷却6小时，运行期间保持一塔吸附和一塔再生。脱水脱碳塔1A/B实际作用是一样，只是两者在同一时间进行的操作不一样。在一个周期内，一个塔吸附，另一个塔再生，进入下一个周期后，两者作用则互换，即A塔再生，B塔吸附。
3.0～7.0MPa的原料天然气与脱水脱碳塔1A相连，经过脱水脱碳塔1A脱水和脱除部分CO2后的干净化气直接进入主换热器3预冷至-40～-65℃左右后，经过低温分离器5分离出的气相进入膨胀机6，膨胀后的气相压力至2.0～4.0MPa后直接进入脱甲烷塔7上部。低温分离器分离出的液相则节流至2.2～4.5MPa后直接进入脱甲烷塔7中部，脱甲烷塔的压力控制在2.8～3.6MPa。脱甲烷塔底部的2.8～3.6MPa C2+则进入后续工序回收乙烷。脱甲烷塔顶部的产品天然气经过主换热器3回收热量后与膨胀机6相连，经过膨胀机同轴增压端增压后的产品气如果不满足外输压力，则大部分(约为80％～93％)再进入产品气压缩机9增压至需要的外输压力(如果膨胀机同轴增压端出口压力满足产品气外输压力则不需产品气压缩机增压)，剩余小部分(约为7％～20％)进入脱水脱碳塔1B，使脱水脱碳塔1B再生，该部分气使脱水脱碳塔再生后，则含有CO2和水，与再生气压缩机2相连，增压至产品气外输需要的压力后与大部分的产品气汇合后一起外输。
本发明中，根据装置的处理能力，所述的脱水脱碳塔可以是两根塔，三根塔或者四根塔。
本发明的原理是：在乙烷回收工厂中，由于乙烷回收装置制冷温度较低，含有一定量CO2的原料天然气极易造成脱甲烷塔冻堵，虽然在脱甲烷塔前端设置一套同样处理量的湿法脱碳装置可以从根本上解决问题，但是该种办法的一次性投资极大，如果在脱水塔中增加一部分脱碳吸附剂，只需将原料气中的CO2降低至一定浓度，则可避免脱甲烷塔冻堵，该种办法仅增加脱水脱碳塔的高度、再生气压缩机功率以及脱水脱碳塔再生相关设备的小部分负荷，一次性投资增加较小。并且再生气压缩机的电负荷较小，因此能耗相比同样处理量的湿法脱碳装置小。管输的原料气中CO2较小时，原料气则不需脱碳可直接进行乙烷回收，也不会造成脱甲烷塔冻堵，该方法针对原料气为管输气的情况时有较高的灵活性。可以应付原料气CO2在一定程度内波动也可以使乙烷回收工厂平稳运行。因此该方法具有投资省，能耗低，操作灵活的优点。

Claims (9)

1.一种在管道天然气中回收乙烷脱二氧化碳的装置，其特征在于：包括两个脱水脱碳塔、主换热器和脱甲烷塔，其中：在两个脱水脱碳塔中增加一部分脱碳吸附剂，两个脱水脱碳塔的顶部进口均与原料天然气管道连接，两个脱水脱碳塔的底部出口均与主换热器连接；所述主换热器与低温分离器连接，所述低温分离器的气相出口依次与膨胀机、脱甲烷塔连接，所述低温分离器的液相出口与脱甲烷塔中部连接；所述脱甲烷塔的顶部出口依次与主换热器、膨胀机相连；两个脱水脱碳塔的底部进口均与膨胀机出口连接；两个脱水脱碳塔的顶部出口均与再生气压缩机连接。
2.根据权利要求1所述的一种在管道天然气中回收乙烷脱二氧化碳的装置，其特征在于：所述主换热器与制冷系统相连。
3.根据权利要求1所述的一种在管道天然气中回收乙烷脱二氧化碳的装置，其特征在于：所述膨胀机与产品气压缩机相连。
4.根据权利要求1所述的一种在管道天然气中回收乙烷脱二氧化碳的装置，其特征在于：在所述脱甲烷塔底部设置重沸器。
5.一种在管道天然气中回收乙烷脱二氧化碳的方法，其特征在于：包括如下内容：3.0～7.0MPa的原料天然气与脱水脱碳塔A相连，经过脱水脱碳塔A脱水和脱除部分CO2后的干净化气进入主换热器预冷至-40～-65℃，然后进入低温分离器进行气液分离，其中：分离出的气相进入膨胀机，膨胀后的气相压力至2.0～4.0MPa后直接进入脱甲烷塔上部；分离出的液相经节流至2.2～4.5MPa后进入脱甲烷塔中部；脱甲烷塔底部的C2+进入后续工序回收乙烷；脱甲烷塔顶部的产品天然气经过主换热器回收热量后与膨胀机相连，经过膨胀机同轴增压端增压后的产品气大部分外输，小部分进入脱水脱碳塔B，使脱水脱碳塔B再生，然后进入再生气压缩机增压至产品气外输需要的压力后与大部分的产品气汇合后一起外输；脱水脱碳塔A和B在一个周期内，一个塔吸附，另一个塔再生，进入下一个周期后，二者互换，运行期间保持一塔吸附和一塔再生。
6.根据权利要求5所述的一种在管道天然气中回收乙烷脱二氧化碳的方法，其特征在于：所述脱甲烷塔的压力为2.8～3.6MPa。
7.根据权利要求5所述的一种在管道天然气中回收乙烷脱二氧化碳的方法，其特征在于：经过膨胀机同轴增压端增压后的大部分外输产品气如果不满足外输压力，进入产品气压缩机增压至需要的外输压力后再外输。
8.根据权利要求5所述的一种在管道天然气中回收乙烷脱二氧化碳的方法，其特征在于：进入脱水脱碳塔B，使脱水脱碳塔B再生的小部分产品气占经过膨胀机同轴增压端增压后的产品气的7%～20%。
9.根据权利要求5所述的一种在管道天然气中回收乙烷脱二氧化碳的方法，其特征在于：在1个操作周期内吸附塔吸附12小时，再生塔再生6小时、冷却6小时。
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