CN104132504A - 一种从井场天然气回收混烃的***及方法 - Google Patents
一种从井场天然气回收混烃的***及方法 Download PDFInfo
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Abstract
本发明属于天然气领域,具体涉及一种从井场天然气回收混烃的***及方法,包括分离增压单元、蒸馏回收单元,可以广泛应用在国内偏远井场气、放空气、站点伴生气的回收具有良好的经济效益和社会效益;HYSYS软件进行模拟分析对已建或将建深冷装置具有实时调整参数、优化参数、提高产率、降低能耗等设计参考价值。
Description
技术领域
本发明属于天然气领域,具体涉及一种从井场天然气回收混烃的***及方法。
背景技术
井场伴生气中除含有甲烷外,含有一定量的乙烷、丙烷、丁烷、戊烷以及更重烃类。为符合商品天然气质量指标或管输气对烃露点的质量要求,或为获得宝贵的液体燃料和化工原料,需将天然气中的烃类按照一定要求分离与回收。
国内一些天然气井场,存在供电、供水设施跟不上,故不适合建造大型天然气处理装置,更适合建造一些小型化和橇装化的混烃回收装置。由于目前国内没有对该工艺进行研究,混烃回收***也缺乏理论知识作为依托。
混烃回收工艺是将C3以上的天然气组分进行充分回收,回收到的天然气凝液或直接作为商品,或根据有关产品质量指标进一步分离为乙烷、液化石油气(LPG),也可以是丙烷、丁烷的混合物)及天然汽油(C5以上)等产品。
发明内容
本发明的目的是提供一种从井场天然气回收混烃的***及方法,该混烃回收工艺方法是将天然气中的丙烷、丁烷等以上重烃回收。
为此本发明提供了一种从井场天然气回收混烃的***,包括分离增压单元、蒸馏回收单元,
1)分离增压单元:包括依次通过管道联接的气液分离器、换热器一、压缩机一、冷却器一、压缩机二、冷却器二、分子筛干燥器,所述分子筛干燥器气体出口联接在换热器一加热管进口,换热器一加热管出口依次联接换热器二节流阀、低温分离器,所述换热器二进口联接低温分离器顶部,所述换热器二出口联接出气管道;
2)蒸馏回收单元:包括脱乙烷塔,所述脱乙烷塔底部联接平衡器,所述平衡器联接出气管道。
所述脱乙烷塔顶部联接在气液分离器下部,所述脱乙烷塔与气液分离器之间还设置有循环器。
所述的换热器一、换热器二为板翅式换热器。
一种从井场天然气回收混烃的方法,包括以下步骤:
1)常温常压下原料气首先进入气液分离器上部,除去其中的水分和杂质;原料气在气液分离器内达到气液相平衡后,分离出的部分气相,温度达到17~18℃,压力达到1.4~1.6MPa,从气液分离器顶部依次进入换热器一,温度达到36~38℃,压力达到1.4~1.6MPa,进入压缩机一,温度达到85~86℃,压力达到2.4~2.5MPa,进入冷却器一,温度达到40~45℃,压力达到2.4~2.5MPa,进入压缩机二,温度达到105~110℃,压力达到4.7~4.9MPa,进入冷却器二,最终温度达到40~45℃,压力4.7~4.9MPa;进入分子筛干燥器脱掉原料气里面的游离水;
2)经过增压和脱水后的原料气,再返回换热器一给原料气提供热量,温度达到20~25℃,压力达到4.5~4.8MPa,再进入换热器二降温至-60~-65℃进入节流阀,节流阀在气体节流处形成局部收缩,使得流速增加、温度和压力降低,降温至-70~-74℃进入低温分离器进行低温闪蒸;
气液分离器操作温度17~18℃,压力1.4~1.6MPa;
3)闪蒸后的原料气温度-70~-75℃,压力3.5~3.8MPa从低温分离器下部进入脱乙烷塔;脱乙烷塔下部产品外输至下游;
脱乙烷塔塔内重沸器中乙烷的摩尔分数控制在5%~15%,脱乙烷塔塔内精馏操作压力1.5~1.7MPa,温度65~70℃。
所述低温分离器顶部出来的气体温度-70~-75℃,压力3.5~4.0MPa,进入换热器二换热后,温度降为15~20℃,压力3.5~4.0MPa外输至下游。
本发明的有益效果是:本发明提供的这一种从井场天然气回收混烃的***及方法,包括分离增压单元、蒸馏回收单元,可以广泛应用在国内偏远井场气、放空气、站点伴生气的回收具有良好的经济效益和社会效益;HYSYS软件进行模拟分析对已建或将建深冷装置具有实时调整参数、优化参数、提高产率、降低能耗等设计参考价值。
下面结合实施例附图对本发明做进一步说明。
附图说明
图1是一种从井场天然气回收混烃的***及方法的实施例示意图;
图中:1、原料气;2、气液分离器;3、换热器一;4、压缩机一;5、冷却器一;6、压缩机二;7、冷却器二;8、分子筛干燥器;9、平衡器;10、脱乙烷塔;11、低温分离器;12、节流阀;13、换热器二;14、循环器。
具体实施方式
实施例1:
如图1所示的一种从井场天然气回收混烃的***,包括分离增压单元、蒸馏回收单元,其特征在于:
1)分离增压单元:包括依次通过管道联接的气液分离器2、换热器一3、压缩机一4、冷却器一5、压缩机二6、冷却器二7、分子筛干燥器8,所述分子筛干燥器8气体出口联接在换热器一3加热管进口,换热器一3加热管出口依次联接换热器二13、节流阀12、低温分离器11,所述换热器二13进口联接低温分离器11顶部,所述换热器二13出口联接出气管道;
2)蒸馏回收单元:包括脱乙烷塔10,所述脱乙烷塔10上部与低温分离器11底部联接,所述脱乙烷塔10底部联接平衡器9,所述平衡器9联接出气管道。
所述脱乙烷塔10顶部联接在气液分离器2下部,所述脱乙烷塔10与气液分离器2之间还设置有循环器14。
所述的换热器一3、换热器二13为板翅式换热器。
一种从井场天然气回收混烃的方法,包括以下步骤:
1)常温常压下原料气1首先进入气液分离器2上部,除去其中的水分和杂质;原料气1在气液分离器2内达到气液相平衡后,分离出的部分气相从气液分离器2顶部依次进入换热器一3、压缩机一4、冷却器一5、压缩机二6,冷却器二7,最终温度达到40~45℃,压力4.7~4.9MPa;进入分子筛干燥器8脱掉原料气(1)里面的游离水;
2)经过增压和脱水后的原料气1,再返回换热器一3给原料气1提供热量,温度达到20~25℃,压力达到4.5~4.8MPa,再进入换热器二13降温至-60~-65℃进入节流阀12,节流阀12在气体节流处形成局部收缩,使得流速增加、温度和压力降低,降温至-70~-74℃进入低温分离器11进行低温闪蒸;
气液分离器(2)操作温度17~18℃,压力1.4~1.6MPa;
3)闪蒸后的原料气1温度-70~-75℃,压力3.5~3.8MPa从低温分离器11下部进入脱乙烷塔10;脱乙烷塔10下部作为产品外输至下游;
脱乙烷塔10塔内重沸器中乙烷的摩尔分数控制在5%~15%,脱乙烷塔10塔内精馏操作压力1.5~1.7MPa,温度65~70℃。
所述低温分离器11顶部出来的气体温度-70~-75℃,压力3.5~4.0MPa,进入换热器二13换热后,温度降为15~20℃,压力3.5~4.0MPa外输至下游。
本发明提供的这一种从井场天然气回收混烃的***及方法,可以广泛应用在国内偏远井场气、放空气、站点伴生气的回收具有良好的经济效益和社会效益。
常温常压下从边远井口出来的原料气1首先进入气液分离器2,在气液分离器2内达到气液相平衡后,分离出部分气相(温度17.8℃,压力1.5MPa),进入板翅式换热器一3,换热后物流温度38℃,压力1.49MPa,进入压缩机一4进行压缩,压缩完物流温度85.3℃,压力2.42MPa,再进入冷却器一5进行冷却,冷却后物流温度40℃,压力2.4MPa,再进入压缩机二6进行压缩,二次压缩后物流温度109℃,压力4.8MPa,再进入冷却器二7进行冷却,二次冷却后物流温度40℃,压力4.8MPa,然后进入分子筛干燥器8脱掉天然气里面的游离水,返回板翅式换热器一3给原料气1温度提供热量,出来物流温度21.6℃,压力4.78MPa,再进入板翅式换热器二13降温至-65℃再进入节流阀12,节流阀12在气体节流处形成局部收缩,使得流速增加温度和压力降低,降温至-73.8℃。节流后的天然气进入低温分离器11进行低温闪蒸。
闪蒸是气相和液相进入容器空间,在一定的压力和温度下,气液两相迅速分离。闪蒸后的物流温度-73.8℃,压力3.8MPa,
进入脱乙烷塔10,脱乙烷塔内重沸器中乙烷的摩尔分数控制在5%~15%,脱乙烷塔内精馏压力控制在1.5MPa~1.52MPa,塔内温度控制在67.4℃,混烃得到大部分回收,经测定混烃的饱和蒸汽压在37.8℃下为0.78MPa,满足液化天然气规范的要求,经平衡器9外输至下游。(规范要求产品混烃饱和蒸汽压≦1.6MPa,常压水露点≦-60℃)。
脱乙烷塔10顶部出来的气相物流温度-58.1℃,压力1.5MPa经过循环器14返回到分离器2;气液分离器2分离出的水由下部排出。
低温分离器11顶部出来的气相物流温度(-70~-75℃,压力3.5~4.0MPa)进入换热器13复热后,物流温度(15~20℃,压力3.5~4.0MPa)外输至下游。
分子筛干燥器8脱出的水由下部排出。
表1是混烃回收产品组分表;表2是外输干气组分表。
表1 混烃回收产品组分表
组分 | CH4 | C2H6 | C3H8 | iC4 | nC4 | iC5 | nC5 | CO2 | N2 |
分数 | 0 | 0.1 | 0.2084 | 0.3356 | 0.0053 | 0.0072 | 0.2312 | 0 | 0 |
表2外输干气组分表
组分 | CH4 | C2H6 | C3H8 | iC4 | nC4 | iC5 | nC5 | CO2 | N2 |
分数 | 0.9157 | 0.022 | 0.0017 | 0.0008 | 0.0001 | 0 | 0 | 0 | 0 |
从表中看出回收的混烃产品中,丙烷以上的组分为78.77%,外输干气中甲烷、乙烷的总组分为93.77%,丙烷以上组分回收率高。
通过对边远井场的天然气组分进行分析,提出了一种混烃回收的***方法。采用国际上著名的HYSYS软件进行模拟分析研究,研究后表明:采用该***所得到的混烃产品(饱和蒸汽压≦1.6MPa,混烃常压水露点≦-60℃)满足规范要求,研究提出的混烃回收***装置能根据不同场站,适应不同气源。该混烃回收***可以广泛应用在国内偏远井场气、放空气、站点伴生气的回收具有良好的经济效益和社会效益。
Claims (5)
1.一种从井场天然气回收混烃的***,包括分离增压单元、蒸馏回收单元,其特征在于:
分离增压单元:包括依次通过管道联接的气液分离器(2)、换热器一(3)、压缩机一(4)、冷却器一(5)、压缩机二(6)、冷却器二(7)、分子筛干燥器(8),所述分子筛干燥器(8)气体出口联接在换热器一(3)加热管进口,换热器一(3)加热管出口依次联接换热器二(13)节流阀(12)、低温分离器(11),所述换热器二(13)进口联接低温分离器(11)顶部,所述换热器二(13)出口联接出气管道;
蒸馏回收单元:包括脱乙烷塔(10),所述脱乙烷塔(10)上部与低温分离器(11)底部联接,所述脱乙烷塔(10)底部联接平衡器(9),所述平衡器(9)联接出气管道。
2.如权利要求1所述的一种从井场天然气回收混烃的***,其特征在于:所述脱乙烷塔(10)顶部联接在气液分离器(2)下部,所述脱乙烷塔(10)与气液分离器(2)之间还设置有循环器(14)。
3.如权利要求1所述的一种从井场天然气回收混烃的***,其特征在于:所述的换热器一(3)、换热器二(13)为板翅式换热器。
4.一种从井场天然气回收混烃的方法,包括以下步骤:
1)常温常压下原料气(1)首先进入气液分离器(2)上部,除去其中的水分和杂质;原料气(1)在气液分离器(2)内达到气液相平衡后,分离出的部分气相,温度达到17~18℃,压力达到1.4~1.6MPa,从气液分离器(2)顶部依次进入换热器一(3),温度达到36~38℃,压力达到1.4~1.6MPa,进入压缩机一(4),温度达到85~86℃,压力达到2.4~2.5MPa,进入冷却器一(5),温度达到40~45℃,压力达到2.4~2.5MPa,进入压缩机二(6),温度达到105~110℃,压力达到4.7~4.9MPa,进入冷却器二(7),最终温度达到40~45℃,压力4.7~4.9MPa;进入分子筛干燥器(8)脱掉原料气(1)里面的游离水;
2)经过增压和脱水后的原料气(1),再返回换热器一(3)给原料气(1)提供热量,温度达到20~25℃,压力达到4.5~4.8MPa,再进入换热器二(13)降温至-60~-65℃进入节流阀(12),节流阀(12)在气体节流处形成局部收缩,使得流速增加、温度和压力降低,降温至-70~-74℃进入低温分离器(11)进行低温闪蒸;
气液分离器(2)操作温度17~18℃,压力1.4~1.6MPa;
3)闪蒸后的原料气(1)温度-70~-75℃,压力3.5~3.8MPa从低温分离器(11)下部进入脱乙烷塔(10);脱乙烷塔(10)下部产品外输至下游;
脱乙烷塔(10)塔内重沸器中乙烷的摩尔分数控制在5%~15%,脱乙烷塔(10)塔内精馏操作压力1.5~1.7MPa,温度65~70℃。
5.如权利要求4所述的一种从井场天然气回收混烃的方法,其特征在于:所述低温分离器(11)顶部出来的气体温度-70~-75℃,压力3.5~4.0MPa,进入换热器二(13)换热后,温度降为15~20℃,压力3.5~4.0MPa外输至下游。
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