CN104964517A - 一种石油伴生气回收lng/lpg/ngl产品的超低温中低压脱氮方法 - Google Patents
一种石油伴生气回收lng/lpg/ngl产品的超低温中低压脱氮方法 Download PDFInfo
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Abstract
本发明具体涉及一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,包括以下步骤:1)原料伴生气增压及净化;2)LPG冷箱流程;3)LNG冷箱流程;4)重烃分馏流程。本发明形成了液化分馏提纯,富氮尾气再利用,重沸器冷箱合一,实现了零排放,能耗较低,运行稳定,满足脱氮工艺要求。
Description
技术领域
本发明具体涉及一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法。
背景技术
伴生气是油田石油伴生气,是原油的挥发性部分,属石油质可燃性气体,为优质燃料和化工原料,主要来源于油井套管、站点气液分离、油罐挥发及原油稳定等等。
以往,由于伴生气分散且量不大,处理工艺复杂,投资较高,大多采取直接或燃烧排放等方式处理,这既污染了环境,也资源了浪费,同时存在安全隐患,与全球节能、减排、低碳经济和绿色发展的理念不相符。
伴生气具有很高的经济价值。伴生气经处理后,可回收的经济产品有:LPG(液化石油气)、NGL(稳定轻烃)和干气(脱轻烃的天然气),干气除作为值班点、加热炉、导热油和发电机的燃料气外,剩余的干气可生产CNG(压缩天然气)和LNG(液化天然气),当气量较大时,也可建设输气管线外销。
在伴生气回收技术方面,国内目前形成了以冷凝分馏、冷油吸收、自产凝液制冷和超音速分离为代表的常规典型工艺,但这些工艺都只生产LPG、NGL和干气,运行温度相对较高,当热值满足要求时对干气中的N2含量没有规定,因此采用常规的伴生气回收技术即可以满足要求。
对于油田伴生气产量较高,地处偏远地区,干气无法自耗且无外输管道,且回收生产LNG产品有较高的经济价值和环保效益,把常规的伴生气回收技术进行深化和拓展,把干气转化生产经济价值较高且便于运输的LNG产品就显得非常必要。
而该工艺技术目前在世界范围内应用业绩和经验都相对缺乏,由于N2的液化温度常压下低至-192℃,比常规天然气的液化温度低约30℃,更难液化,因此生产LNG产品对N2含量的要求较为严格,当N2含量超过一定限值时,LNG产品储存过程中在储罐内易出现“翻滚”现象而影响其的储存安全,同时LNG的蒸发将显著,BOG气体量较大,回收BOG气体的投资和能耗都将上升。
干气脱N2存在的问题主要体现在下述三个方面:①采用常规的变压吸附脱N2工艺,存在二次增压的问题,设备较多、流程复杂、操作不便、运行稳定性较差、投资高等缺点;②采用常规的低温溶剂吸收脱N2工艺,存在二次脱重烃、二次增压的问题,设备较多、流程复杂、操作不便、运行稳定性较差、投资高等缺点;③采用常规的超低温精馏脱氮工艺,需要采用高压、低压两个塔进行变压操作,且最低温度达到-187℃,冷位温度对制冷剂要求较高,冷量消耗较大。
发明内容
本发明的目的是避免LNG产品在储罐中出现“翻滚”现象而影响安全储存,降低LNG的蒸发损耗,减少BOG气体,降低工程投资和运行费用。
为此,本发明提供了一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,包括以下步骤:
步骤1)原料伴生气增压及净化:原料伴生气从管路依次进入一级分离器、一级压缩机、二级分离器、脱硫脱碳塔、一级分子筛脱水装置、精脱硫吸附塔、二级压缩机、三级分离器进行气液分离、一级增压、脱硫脱碳、脱水、精脱硫、二级增压后形成高压净化伴生气;
步骤2)LPG冷箱流程:高压净化伴生气从三级分离器顶部进入LPG冷箱下部进行初步冷却,冷却后进入重烃洗涤塔,从重烃洗涤塔的上部产生低温伴生气,下部产生低温凝液,低温凝液进入重烃分馏流程;
步骤3)LNG冷箱流程:低温伴生气经重烃洗涤塔的上部进入二级分子筛脱水装置后进入LNG冷箱,在超低温 -150℃~-160℃、压力1.0~3.0MPa下液化形成液态富氮LNG,液态富氮LNG进入脱氮提馏塔上段,脱氮提馏塔下部的富氮LNG作为重沸物流通过管路再经过LNG冷箱升温至-105℃,重沸物流加热后部分汽化成气态富氮LNG再进入脱氮提馏塔下段,通过气态富氮LNG上升与下降的液态富氮LNG逆向接触,气提出富氮LNG中的N2,产生的低温富氮尾气经脱氮提馏塔顶部排出,产生的贫氮LNG经脱氮提馏塔底部排出后再经过LNG冷箱后得到LNG产品,最后进入LNG储罐储存;
步骤4)重烃分馏流程:步骤2)中的低温凝液进入脱乙烷塔,脱乙烷塔的顶部产生冷富甲烷气,底部产生混烃,混烃进入脱丁烷塔上段后,在脱丁烷塔底部产生NGL产品,顶部排出LPG产品。
脱氮提馏塔底部排出的贫氮LNG分为两路,一路经过LNG冷箱后得到LNG产品,另一路经过LNG冷箱后进入LPG制冷剂压缩机,压缩后进入LPG冷箱作为LPG冷箱制冷剂,然后再经管路进入LNG冷箱冷却,如此循环往复为LPG冷箱提供制冷剂。
脱乙烷塔的顶部产生的冷富甲烷气通过管线进入LPG冷箱,将冷量交换后排出常温富甲烷气为LPG冷箱提供制冷剂。
脱氮提馏塔顶部的低温富氮尾气经管线进入LNG冷箱,将冷量交换后排出常温富氮尾气。
本发明与现有技术相比,具有以下特点:
①将具有一定压力的伴生气经过降温液化,利用甲烷等轻烃类物质与N2的相对挥发度不同,用分馏的方法脱出N2;
②采用单塔工艺,只设置提馏段以保证塔底LNG产品N2的含量低于2%,塔顶富氮尾气N2含量达到80%,甲烷含量为20%,低温富氮尾气作为制冷剂的原料,多余部分由于量少可补充至燃料气***,以最大程度减少对环境的排放;
③利用LNG冷箱,对冷量进行充分回收,脱氮提馏塔下段重沸物流在升温的同时也作为冷源,脱氮提馏塔顶的低温富氮尾气也利用了LNG冷箱回收了冷量,节能效果显著。
下面将结合附图做进一步详细说明。
附图说明
图1是本发明的总流程示意图;
图2是脱氮流程示意图。
图中:1、原料伴生气;2、一级分离器;3、一级压缩机;4、二级分离器;5、脱硫脱碳塔;6、一级分子筛脱水装置;7、精脱硫吸附塔;8、二级压缩机;9、三级分离器;10、高压净化伴生气;11、LPG冷箱;12、重烃洗涤塔;13、二级分子筛脱水装置;14、LNG冷箱;15、液态富氮LNG;16、脱氮提馏塔;17、低温富氮尾气;18、LNG储罐;19、LNG产品;20、装车泵;21、BOG气;22、低温凝液;23、低温伴生气;24、脱乙烷塔;25、混烃;26、冷富甲烷气;27、脱丁烷塔;28、NGL产品;29、LPG产品;30、LNG制冷剂压缩机;31、LPG制冷剂压缩机;32、贫氮LNG;33、重沸物流;34、贫胺液;35、富胺液;36、高压低温Ⅰ级制冷剂;37、常温富氮尾气;38、气态富氮LNG;39、低压常温Ⅰ级制冷剂;40、高压低温Ⅱ级制冷剂;41、低压常温Ⅱ级制冷剂;42、常温富甲烷气。
具体实施方式
实施例1:
本实施例提供了一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,该石油伴生气气源来至原油田联合站的放空火炬管线,压力极低,仅为13kPa,原料伴生气中重烃含量较高、含较高的硫化氢且含有一定量的硫醇,含有二氧化碳和饱和水,所以总工艺流程图中包括了原料伴生气增压及净化、LPG冷箱流程、LNG冷箱流程、重烃分馏流程,如图1、2所示,包括以下步骤:
步骤1)原料伴生气增压及净化:原料伴生气1从管路依次进入一级分离器2、一级压缩机3、二级分离器4、脱硫脱碳塔5、一级分子筛脱水装置6、精脱硫吸附塔7、二级压缩机8、三级分离器9进行气液分离、一级增压、脱硫脱碳、脱水、精脱硫、二级增压后形成高压净化伴生气10;其中,脱硫脱碳塔5通过塔上部进入的贫胺液34吸收原料伴生气1中的硫化氢和二氧化碳,富胺液35从塔底部排出,精脱硫吸附塔7原理是利用活性炭石化无碱脱硫醇;
步骤2)LPG冷箱11流程:高压净化伴生气10从三级分离器9顶部进入LPG冷箱11下部进行初步冷却,冷却后进入重烃洗涤塔12,从重烃洗涤塔12的上部产生低温伴生气23,下部产生低温凝液22,低温凝液22进入重烃分馏流程;
步骤3)LNG冷箱14流程:低温伴生气23经重烃洗涤塔12的上部进入二级分子筛脱水装置13后进入LNG冷箱14,在超低温 -150℃~-160℃、压力1.0~3.0MPa下液化形成液态富氮LNG15,液态富氮LNG15进入脱氮提馏塔16上段,脱氮提馏塔16下部的富氮LNG作为重沸物流33通过管路再经过LNG冷箱14升温至-105℃,重沸物流33加热后部分汽化成气态富氮LNG38再进入脱氮提馏塔16下段,通过气态富氮LNG38上升与下降的液态富氮LNG15逆向接触,气提出富氮LNG中的N2,产生的低温富氮尾气17经脱氮提馏塔16顶部排出,产生的贫氮LNG32经脱氮提馏塔16底部排出后再经过LNG冷箱14后得到LNG产品19,然后进入LNG储罐18储存,在LNG储罐18的顶部排出BOG气21,最后通过装车泵20灌装;
步骤4)重烃分馏流程:步骤2)中的低温凝液22进入脱乙烷塔24,脱乙烷塔24的顶部产生冷富甲烷气26,底部产生混烃25,混烃25进入脱丁烷塔27上段后,在脱丁烷塔27底部产生NGL产品28,顶部排出LPG产品29。
通过本实施例提供的方法将具有一定压力的伴生气经过降温液化,利用甲烷等轻烃类物质与N2的相对挥发度不同,用分馏的方法脱出N2;采用单塔工艺,只设置提馏段以保证脱氮提馏塔16塔底LNG产品19 N2的含量低于2%,塔顶富氮尾气N2含量达到80%,甲烷含量为20%。
实施例2:
在实施例1的基础上本发明还包括制制冷剂循环流程,如图1、2所示,分为LPG冷箱制冷剂循环和LNG冷箱制冷剂循环;
LPG冷箱制冷剂循环具体过程为:
(1)脱氮提馏塔16底部排出的贫氮LNG32分为两路,一路经过LNG冷箱14后得到LNG产品19,另一路经过LNG冷箱14后进入LPG制冷剂压缩机31,压缩后进入LPG冷箱11作为LPG冷箱制冷剂,然后再经管路进入LNG冷箱14冷却,如此循环往复为LPG冷箱11提供制冷剂;
(2)脱乙烷塔24的顶部产生的冷富甲烷气26通过管线进入LPG冷箱11,将冷量交换后排出常温富甲烷气42;
LNG冷箱制冷剂循环具体过程为:
(1)制冷剂由LNG制冷剂压缩机30压缩后进入LNG冷箱14作为LNG冷箱制冷剂,然后再进入LNG制冷剂压缩机30压缩,如此循环往复为LNG冷箱14提供制冷剂;
(2)脱氮提馏塔16顶部的低温富氮尾气17经管线进入LNG冷箱14,将冷量交换后排出常温富氮尾气37;
其中,LNG冷箱14分为上下两部分,制冷剂分为Ⅰ级制冷剂和Ⅱ级制冷剂,上部制冷剂为Ⅰ级制冷剂,使LNG冷箱14温度维持在-105℃,Ⅰ级制冷剂经LNG制冷剂压缩机30后成为高压低温Ⅰ级制冷剂36,冷量交换后成低压常温Ⅰ级制冷剂39,下部为Ⅱ级制冷剂,使LNG冷箱14温度维持在-150℃~-160℃,Ⅱ级制冷剂经LNG制冷剂压缩机30后成为高压低温Ⅱ级制冷剂40,冷量交换后成低压常温Ⅱ级制冷剂41。
实施例3:
将本发明应用于俄罗斯某油田联合站燃烧排放的伴生气的回收项目,生产LNG、LPG、NGL等经济产品,具有很好的环境效益和经济效益,原料伴生气1中氮气含量高达7.8%,处理规模为5.7×104m3/d(20℃,101.325kPa),理论可生产LNG共29t/d,LPG共21.7t/d和NGL共8.7t/d,LNG产品19中N2含量低于2%。
综上所述,本发明形成了液化分馏提纯,富氮尾气再利用,重沸器冷箱合一,实现了零排放,能耗较低,运行稳定,满足脱氮工艺要求。
本实施例没有详细叙述的产品性能测试方法属本行业的公知或常用测试方法,这里不一一叙述。
以上例举仅仅是对本发明的举例说明,并不构成对本发明的保护范围的限制,凡是与本发明相同或相似的设计均属于本发明的保护范围之内。
Claims (4)
1.一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,其特征在于,包括以下步骤:
步骤1)原料伴生气(1)增压及净化:原料伴生气(1)从管路依次进入一级分离器(2)、一级压缩机(3)、二级分离器(4)、脱硫脱碳塔(5)、一级分子筛脱水装置(6)、精脱硫吸附塔(7)、二级压缩机(8)、三级分离器(9)进行气液分离、一级增压、脱硫脱碳、脱水、精脱硫、二级增压后形成高压净化伴生气(10);
步骤2)LPG冷箱流程:高压净化伴生气(10)从三级分离器(9)顶部进入LPG冷箱(11)下部进行初步冷却,冷却后进入重烃洗涤塔(12),从重烃洗涤塔(12)的上部产生低温伴生气(23),下部产生低温凝液(22),低温凝液(22)进入重烃分馏流程;
步骤3)LNG冷箱流程:低温伴生气(23)经重烃洗涤塔(12)的上部进入二级分子筛脱水装置(13)后进入LNG冷箱(14),在超低温 -150℃~-160℃、压力1.0~3.0MPa下液化形成液态富氮LNG(15),液态富氮LNG(15)进入脱氮提馏塔(16)上段,脱氮提馏塔(16)下部的富氮LNG作为重沸物流(33)通过管路再经过LNG冷箱(14)升温至-105℃,重沸物流(33)加热后部分汽化成气态富氮LNG(38)再进入脱氮提馏塔(16)下段,通过气态富氮LNG(38)上升与下降的液态富氮LNG(15)逆向接触,气提出富氮LNG中的N2,产生的低温富氮尾气(17)经脱氮提馏塔(16)顶部排出,产生的贫氮LNG(32)经脱氮提馏塔(16)底部排出后再经过LNG冷箱(14)后得到LNG产品(19),最后进入LNG储罐(18)储存;
步骤4)重烃分馏流程:步骤2)中的低温凝液(22进入脱乙烷塔(24,脱乙烷塔(24)的顶部产生冷富甲烷气(26),底部产生混烃(25),混烃(25)进入脱丁烷塔(27)上段后,在脱丁烷塔(27)底部产生NGL产品(28),顶部排出LPG产品(29)。
2.根据权利要求1所述的一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,其特征在于:脱氮提馏塔(16)底部排出的贫氮LNG(32)分为两路,一路经过LNG冷箱(14)后得到LNG产品(19),另一路经过LNG冷箱(14)后进入LPG制冷剂压缩机(31),压缩后进入LPG冷箱(11)作为LPG冷箱制冷剂,然后再经管路进入LNG冷箱(14)冷却,如此循环往复为LPG冷箱(11)提供制冷剂。
3.根据权利要求1所述的一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,其特征在于:脱乙烷塔(24)的顶部产生的冷富甲烷气(26)通过管线进入LPG冷箱(11),将冷量交换后排出常温富甲烷气(42)为LPG冷箱(11)提供制冷剂。
4.根据权利要求1所述的一种石油伴生气回收LNG/LPG/NGL产品的超低温中低压脱氮方法,其特征在于:脱氮提馏塔(16)顶部的低温富氮尾气(17)经管线进入LNG冷箱(14),将冷量交换后排出常温富氮尾气(37)。
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