CN100408954C - 提高ngl回收率的装置和方法 - Google Patents
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Abstract
将改进的NGL处理装置中的原料气(1)冷却到低于环境温度并高于原料气的水合点温度,以凝结原料气中所含的重成分(6)和大部分水(4)。水(4)在原料气分离器(101)中除去,将冷凝的液体送入作为冷凝液体的干燥器/脱甲烷塔运行的集成的回流汽提塔(104)中,并在汽轮膨胀(23)和脱甲烷反应(112)之前进一步干燥(106)和冷却含有轻成分的未凝结部分(5)。最终取消了冷却段中重成分的处理,并使组分范围宽的原料气能在基本上相同的操作条件和最佳的膨胀器效率下以高的NGL回收率进行有效的处理。
Description
本申请要求2001年11月9日提出的序列号为60/337481的美国临时专利申请的权益,将其引入本文作为参考。
发明领域
本发明领域是从原料气回收气体汽油(NGL)。
发明背景
从各种原料气回收NGL在经济上变得越来越有吸引力,现有技术中有许多公知的提高原料气的NGL回收率的处理装置和方法。典型实例包括Campbell等人的US 4157904、Gulsby的US 4251249、Buck的US 4617039、Paradowski等人的US 4690702、Campbell等人的US5275005、Wilkinson等人的US 5799507和Rambo等人的US 5890378中描述的低温膨胀装置和方法。
然而,虽然所有这些方法都表现出较高的NGL回收率,但仍存在许多困难。别的不说,采用低温膨胀的NGL回收方法一般要求使用汽轮膨胀器,使原料气冷却,以提高丙烷或乙烷回收率。而且许多公知的NGL回收方法设计成在特定入口条件下处理特定的气体组成。因此当原料气组成改变时,NGL回收率一般会降低,丧失了潜在的产品收益。为了保持高NGL回收率,往往需要对现有单元的设备进行昂贵的改进。此外,由于需要对整个原料气进行干燥(例如使用分子筛),以防止水分在低温段冷冻溢出,这种装置往往需要较高的干燥成本。因此开发了各种优化措施。例如Campbell等在US 6182469中描述了将干燥原料气在使用冷干气的换热器和侧再热器中冷却,如现有技术图1中所叙述的。然后在分离器中分离出冷凝液体并送入脱甲烷塔中。作为选择,如Sorensen在US 5953935中所描述的,可在脱甲烷塔上游增加吸收器,如现有技术图2中所叙述的。在这种装置中,来自原料分离器和吸收器底部的液体被送到脱甲烷塔。为了提高NGL回收率,通过用脱甲烷塔塔顶蒸气冷却来冷却并回流吸收器塔顶馏分。
在另一种公知的装置中,如Lee等的US 6244070和Foglietta的US 5890377中描述的,再热器负荷集成到原料冷却中,在这些装置中,来自中间分离器的液体被送入下游脱甲烷塔中的不同位置进行NGL回收。这些方法还包括提供冷却NGL方法的各种措施。根据Elliott和Foglietta的装置的实例分别叙述在现有技术图3和4中。
这种优化的装置一般将NGL回收率提高到至少某一程度。然而,明显的处理限制依然存在。最明显的是,由于从中间冷却步骤分离出的液体被送入脱甲烷塔,这种装置通常对于相对具体和窄范围的原料气组分有最高的运行效率。因此当原料气组分改变时,尤其是当原料气含有更多的C5(+)成分时,NGL回收率将显著降低,且能耗将提高(一般是由于额外的C5(+)成分提高了NGL回收单元的操作温度,从而导致汽轮膨胀器和脱甲烷塔的运行效率降低)。
因此,尽管有各种公知的从原料气回收NGL的装置和方法,它们所有或几乎所有都存在一种或多种缺点。因此仍需要提供提高NGL回收率的装置和方法。
本发明概述
本发明涉及NGL回收装置和构型,其中将原料气冷却,以从原料气除去至少部分水和C5(+)液体,从而保持较贫乏的气体至下游单元。设想的装置包括将至少部分干燥过的气体分离成C5(+)贫化气体和C3(+)液体的中间分离器。设想的装置还包括接收至少部分C5(+)贫化气体的汽轮膨胀器,以及接收来自原料分离器的C5(+)液体、并进一步接收来自中间分离器的C3(+)液体作为回流物的回流汽提塔。
特别优选的装置还包括接收并干燥来自原料分离器的气体,从而产生至少部分脱了水的气体的气体干燥器,至少部分脱了水的气体通过第一换热器和第二换热器的至少一个进一步冷却(其中在第一换热器中的冷却通过从脱甲烷塔的再热器循环提供,而其中在第二换热器中的冷却通过脱甲烷塔的塔顶馏出物提供)。此外,设计另一部分C5(+)贫化气体可通过第三换热器冷却(其中在第三换热器中的冷却通过脱甲烷塔的塔顶馏出物提供),作为脱甲烷塔的回流物使用。
在另一个设计的装置中,回流的汽提塔包括脱水段(最优选的是包含蒸气-TEG接触装置的三甘醇(TEG)脱水段)。对于原料分离器,设计的是,原料分离器接收冷却到高于该气体水合点温度的原料气,且原料分离器进一步从原料气中分离出至少一部分该原料气所含水分。在特别优选的装置中的原料气将含有乙烷、丙烷和较重的成分,其中对原料气中乙烷和丙烷的回收率分别为至少87%和97%。
在本发明目的的另一个方面,设计的装置将包括接收C5(+)贫化气体(例如通过中间分离器提供)的脱甲烷塔,其中C5(+)贫化气体的第一部分在汽轮膨胀器中膨胀,而其中C5(+)贫化气体的第二部分被冷却,并用作脱甲烷塔回流物。在这种装置中,设计的是,原料分离器将原料气分离成C5(+)贫化气体部分和液体部分,其中C5(+)贫化气体部分在中间分离器中被冷却和分离,从而产生C5(+)贫化气体。
在本发明目的进一步的方面,该装置包含接收水饱和的C5(+)液体的回流汽提塔,还包含中间塔脱水段,其中回流汽提塔作为脱甲烷塔运行,且其中回流汽提塔接收来自中间分离器的回流物,中间分离器向脱甲烷塔提供C5(+)贫化气体。
本发明的各种目的、特征、方面和优点将从本发明优选实施方案的以下详细描述和附图中变得更清楚。
附图简述
现有技术图1是一个公知的NGL回收装置的简图,其中干燥原料气在换热器中用冷干气和侧再热器进行冷却。
现有技术图2是另一个公知的NGL回收装置的简图,其中吸收器装置在脱甲烷塔上游。
现有技术图3仍是另一个公知的NGL回收装置的简图,其中再热器和原料气压缩集成在原料冷却器中。
现有技术图4还是另一个公知的NGL回收装置的简图,其中再热器和压缩的干气循环集成在原料冷却器中。
图5是根据本发明目的的NGL回收装置实例的简图。
图6是根据本发明目的的NGL回收装置实例中气体流的计算组分列表。
详细描述
本发明人发现,在处理各式各样的气体组分的装置中可实现高效NGL回收,且当原料气相对富含C2和C3(+)成分时,设计的装置特别高效(即低能耗下较高的回收率)。而且特别设计的装置将显著降低脱水能耗,而且还消除了装置冷却段的原料气中高沸点组分的处理。
尤其优选的装置叙述在图5中,其中含有图6的表中所示典型组分的湿原料气1通过原料气冷却器100,在高压(例如约800psig-约1400psig)下由制冷剂2冷却到正好高于水合物形成点(一般约55°F-约65°F)。下游原料分离器101(优选的是三相分离器)除去冷却的原料气3中的水4,从而降低下游脱水单元和低温设备的尺寸和能耗。原料分离器101将冷却的原料气3进一步分离成液体部分6和蒸气部分5。液体部分6在换热器102中预热成液流7,通过JT阀103减压排出并送入回流汽提塔104。汽提塔塔底产物10包含含有几乎全部是C5(+)成分的NGL产物,并用于预热换热器102中的原料液体6。
关于回流汽提塔的装置,可以理解的是,汽提塔是具有下部汽提段、中部脱水段和上部吸收段的集成容器。中间段包括采用合适干燥介质(例如三甘醇(TEG))的脱水托盘,以制备干燥气体(例如约-40°F水露点)。采用脱水段干燥尤其是有益的,因为来自原料分离器101的液体通常是含水饱和的,如果不脱水,它在上段中就可能冻结。上部吸收段一般在约-5°F--35°F下运行,并回流来自中间分离器109的冷的富C3(+)液体20。
在回流汽提塔的上段中,作为更冷液体的回流流体20将凝结,并吸收来自中间段的干燥蒸气中的大部分C3(+)成分。富C3(+)液体收集到上段的烟囱托盘中,并通过TEG部分的旁路流入下部汽提段。该物流在图5中示为物流38。
设计的汽提塔的运行压力一般在约300-450psig范围,设想的运行温度一般在上段中为约-5°F--35°F范围,在下段中为250°F-350°F。汽提塔塔顶气体9主要是甲烷含量约为50-70mol%的干气。塔顶气体9中所含的制冷剂可用于在干气换热器108中冷却原料气16。
来自原料分离器101的蒸气流5在干燥单元106(优选采用分子筛)中干燥,以制备物流15,并进一步分隔成两股物流16和17。物流16在干气换热器108中用脱甲烷塔塔顶物流28和汽提塔塔顶蒸气9冷却到约-10°F-10°F。物流17在再热换热器107中用脱甲烷塔侧馏分物流34和35冷却到约-10°F-10°F。然后将这样干燥和冷却的蒸气部分送入中间分离器109(一般是膨胀器抽吸鼓)。
富C3(+)液体20在中间分离器109中从干燥和冷却的蒸气部分18和19中分离出,经JT阀117减压排出,并作为冷回流液送入回流汽提塔104塔顶。特别应该认识到的是,在所有以前公知的方法中,中间分离器液体总是送入诸如脱甲烷塔的下游塔中。相反,设计的装置却将中间分离器液体送入上游塔即回流汽提塔中,这在要求高的NGL回收率时尤其有价值。来自中间分离器的富C5(+)液体20最适合用于从原料分离器液体6回收C3(+)成分,制备C3(+)贫化成分的非常贫乏的汽提塔塔顶气体9。
在中间分离器109中从干燥和冷却的蒸气流18和19中分离出C5(+)贫化蒸气21。流体21分成物流22和物流23两部分。占物流21的约40-60%的物流23在进入脱甲烷塔112前先在汽轮膨胀器110中膨胀成物流24,而物流22则通过回流换热器111(用脱甲烷塔塔顶蒸气26作为制冷剂)进一步冷却成物流25并经JT阀118减压排出,以提供脱甲烷塔回流物流40。回流换热器111排出的脱甲烷塔塔顶蒸气的制冷剂成分可进一步用于第二换热器中(例如中间分离器109上游的干气换热器108),而脱甲烷塔塔底产物27包含需要的NGL产物(它可在与汽提塔塔底产物10混合前通过JT阀减压排入物流13,形成NGL产物流14)。
来自换热器108的加热过的干气蒸气28与汽提塔塔顶蒸气物流29混合从而形成物流30,并将其加入到由汽轮膨胀器110驱动的压缩机中,将该气体压缩成物流31。物流31由干气压缩机114进一步压缩成物流32,该物流在作为物流33输送到出售气体管线之前由空气冷却器115进一步冷却。
本文所用术语“富C5(+)”液体、蒸气或其他馏分指该液体、蒸气或其他馏分含有比衍生出该富C5(+)液体、蒸气或其他馏分的液体、蒸气或其他馏分更高摩尔分数的C5、C5异构重整体和/或更重的成分。同样,本文所用术语“C5(+)贫化”液体、蒸气或其他馏分指该液体、蒸气或其他馏分含有比衍生出该C5(+)贫化液体、蒸气或其他馏分的液体、蒸气或其他馏分更低摩尔分数的C5、C5异构重整体和/或更重的成分。
对于原料气体,一般设计的是,合适的原料气包括乙烷和丙烷,并可进一步含有二氧化碳。因而,应该理解的是,原料气的性质可以有很大不同,且装置中的所有原料气都认为是合适的,只要它们含有C2和C3成分,更一般的C1-C5成分,最一般的C1-C6(+)成分即可。因此,尤其优选的原料气包括天然气、炼油厂气,以及由诸如煤、原油、石脑油、油页岩、焦油砂和褐煤的其他烃材料得到的合成气流。合适的气体还可含有较少量的诸如丙烷、丁烷、戊烷等的较重的烃,以及氢、氮、二氧化碳和其他气体。
根据原料气的具体来源和性质不同,应该认识到,原料气的冷却可有很大不同。然而,通常优选的是将原料气冷却到高于(一般高约5°F,更一般的高约10°F)原料气水合点的温度。因此,在原料气为天然气的情况下,例举冷却的原料气温度将为约55°F至约65°F。同样,根据具体的原料气,原料气的压力可有显著的变化。然而,通常优选的是原料气具有约800psig至约1400psig,更一般的约1000psig至约1400psig的压力。
现有技术中有许多合适的原料分离器,一般设想所有这些原料分离器都是合适的。然而,尤其优选的原料分离器包括三相分离器,其中可从烃类液体和蒸气相中分离出水。进一步设想用于本发明装置中的脱甲烷塔、换热器、干燥器、干气压缩机和汽轮膨胀器是本领域普通技术人员公知的常用装置。中间分离器最优选的是膨胀器抽吸鼓。然而,作为选择的中间分离器将包括从C5(+)贫化蒸气分离出凝结的富C5(+)液体的所有分离器。
在设计装置的其他优点中,尤其应该认识到的是,中间分离器从原料气的预干燥蒸气部分制备了富C5(+)液体和C5(+)贫化蒸气。因此这样制备的富C5(+)液体可有益地用作作为脱甲烷塔运行的汽提塔的回流物,以显著提高NGL回收率。而且由于送入汽轮膨胀器中的蒸气部分是C5(+)贫化蒸气,汽轮膨胀器和下游脱甲烷塔的运行将基本上不受原料气组成波动的影响。
仍然应该进一步认识到的是,通过使用原料冷却器和原料分离器,以及来自原料冷却器的蒸气的进一步冷却和冷蒸气在中间分离器中的分离(以形成富C5(+)液体和C5(+)贫化蒸气),可从原料气中除去即使不是所有也是大部分的较重成分。从而使流过冷却段的材料组成大体上稳定,因为在NGL装置的冷却段中原料气中重成分的处理可以省去。因此,热负载、汽轮膨胀器和脱甲烷塔将运行在最有效的点,而与原料气组分的变化无关。这样,设计的装置和方法就能简单和灵活地处理变化的原料气流量和气体组成,从而降低汽轮膨胀器在常规设计中的不同气体组成下运行的复杂程度。从另一方面看,设计的方法通过除去原料气中的重成分而使NGL回收装置保持在恒定的条件下运行。根据先前完成的计算(数据未示出),设计的装置将达到至少80%,更典型的是87%的乙烷回收率,和至少95%,和更典型的是97%的丙烷回收率(见图6)。
更进一步说,由于原料气中的大部分(一般为约60%至约95%,更典型的为约75%至约90%)水在原料分离器中被除去,使原料气脱水能耗显著降低。
因此,本发明人设计了一种装置,它包括(1)冷却含有水和C5(+)成分的原料气的原料冷却器,和从冷却的原料气中除去至少部分水和C5(+)成分的原料气分离器,(2)与原料分离器呈流体连通、并将至少部分脱了水的气体分离成C5(+)贫化气体和C3(+)液体的中间分离器,(3)接收至少部分C5(+)贫化气体的汽轮膨胀器,和(4)接收来自原料分离器的C5(+)液体、并进一步接收来自中间分离器的C3(+)液体作为回流物的回流汽提塔(吸收、脱水和汽提段集成在单个塔中)。在特别优选的装置中,气体干燥器接收并干燥来自原料分离器的气体,从而产生至少部分脱了水的气体,而至少部分脱了水的气体通过第一换热器和第二换热器中的至少一个进一步冷却,其中第一换热器中的冷却通过来自脱甲烷塔的再热器回路提供,而其中第二换热器中的冷却通过脱甲烷塔的塔顶馏出物提供。C5(+)贫化气体的另一部分可通过第三换热器冷却,其中第三换热器中的冷却通过脱甲烷塔的塔顶馏出物提供,且其中冷却的C5(+)贫化气体部分的另一部分用作脱甲烷塔回流物。
在设计装置的另一方面,该装置可包括接收C5(+)贫化气体的脱甲烷塔,其中C5(+)贫化气体的第一部分在汽轮膨胀器中膨胀,且其中C5(+)贫化气体的第二部分通过中间分离器提供,被冷却并用作脱甲烷塔回流物,其中原料分离器将原料气分离成C5(+)贫化气体部分和液体部分,且其中C5(+)贫化气体部分在中间冷却器中冷却并分离,从而制备C5(+)贫化气体。
在这种装置中,通常优选的是气体干燥器(最优选的是使用分子筛)在冷却前先于燥C5(+)贫化气体部分,且C5(+)贫化气体部分通过第一换热器和第二换热器中的至少一个冷却,其中第一换热器中的冷却通过来自脱甲烷塔的再热器回路提供,而其中第二换热器中的冷却通过脱甲烷塔的塔顶馏出物提供。C5(+)贫化气体第二部分的冷却可通过第三换热器提供,且其中第三换热器中的冷却通过脱甲烷塔的塔顶馏出物提供。
在设计装置的又一个方面,该装置包括接收水饱和的C5(+)液体的回流汽提塔,还包括上部吸收段、中间塔脱水段和下部汽提段,其中汽提塔作为脱甲烷塔运行,且其中汽提塔接收来自中间分离器的回流物,并向脱甲烷塔提供C5(+)贫化气体。在这种装置中,优选的是中间分离器接收在原料气分离器中从原料气分离出的至少部分脱了水的气体,且其中该原料气分离器还制备水饱和的C5(+)液体。
这样就已经公开了用于提高NGL回收率的装置和方法的具体实施方式和应用。然而本领域普通技术人员应该明白的是,除已描述的那些以外的更多改进都是可能的,而不脱离本发明的范围。因此本发明的主题除附属权利要求的精神以外不受限制。而且,在说明书和权利要求的解释中,所有术语都应以与上下文一致的最广泛可能的方式进行解释。具体说,术语“包括”和“包含”应解释成以非限定性方式指部件、成分或步骤,指提及的部件、成分或步骤可存在或利用,或与未明确提及的其他部件、成分或步骤结合。
Claims (21)
1. 一种装置,包括
冷却含有水和C5(+)成分的原料气的原料冷却器,和从冷却的原料气中除去至少部分水和C5(+)成分的原料分离器;
与该原料分离器呈流体连通,并将至少部分脱水的气体分离成C5(+)贫化气体和C3(+)液体的中间分离器;
接收至少部分该C5(+)贫化气体的汽轮膨胀器;和
包括吸收段、脱水段和汽提段,并接收来自该原料分离器的C5(+)液体和进一步接收来自该中间分离器的C3(+)液体作为回流物的回流汽提塔。
2. 权利要求1的装置,还包括接收并干燥来自原料分离器的气体,从而产生至少部分脱了水的气体的干燥单元。
3. 权利要求2的装置,还包括第一换热器、第二换热器、脱甲烷塔和来自脱甲烷塔的再热器回路,其中至少部分脱了水的气体通过第一换热器和第二换热器中的至少一个进一步冷却,其中第一换热器中的冷却通过来自脱甲烷塔的再热器回路提供,且其中第二换热器中的冷却通过脱甲烷塔的塔顶馏出物和来自汽提塔的塔顶馏出物气体提供。
4. 权利要求3的装置,还包括第三换热器,其中C5(+)贫化气体部分的另一部分通过该第三换热器冷却,其中第三换热器中的冷却通过脱甲烷塔的塔顶馏出物提供,且其中冷却的C5(+)贫化气体部分的另一部分用作脱甲烷塔的回流物。
5. 权利要求1的装置,其中原料分离器是三相分离器。
6. 权利要求1的装置,其中脱水段包括包含蒸气-TEG接触装置的三甘醇脱水段。
7. 权利要求1的装置,其中原料冷却器将原料气冷却到高于水合点的温度。
8. 权利要求7的装置,其中原料气是天然气。
9. 权利要求7的装置,其中原料气包含乙烷、丙烷和较重的成分,且其中原料气中乙烷和丙烷的回收率分别至少为87%和97%。
10. 权利要求1的装置,包括
接收来自中间分离器的C5(+)贫化气体的脱甲烷塔,其中该C5(+)贫化气体的第一部分在汽轮膨胀器中膨胀,且其中该C5(+)贫化气体的第二部分被冷却并用作脱甲烷塔回流物;
其中原料分离器将原料气分离成C5(+)贫化气体部分和液体部分;和
其中所述C5(+)贫化气体部分在该中间分离器中冷却并分离,从而制备C5(+)贫化气体。
11. 权利要求10的装置,还包括在冷却前干燥C5(+)贫化气体部分的干燥单元。
12. 权利要求11的装置,还包括第一换热器、第二换热器和来自脱甲烷塔的再热器回路,其中C5(+)贫化气体部分通过第一换热器和第二换热器中的至少一个冷却,其中第一换热器中的冷却通过来自脱甲烷塔的再热器回路提供,且其中第二换热器中的冷却通过脱甲烷塔的塔顶馏出物和来自汽提塔的塔顶馏出物气体提供。
13. 权利要求11的装置,还包括第三换热器,其中第二部分C5(+)贫化气体的冷却通过该第三换热器提供,且其中第三换热器中的冷却通过脱甲烷塔的塔顶馏出物提供。
14. 权利要求11的装置,还包括接收来自原料分离器的液体部分的汽提塔,且其中汽提塔还接收来自中间分离器的C3(+)液体作为回流物。
15. 权利要求14的装置,其中汽提塔还包括脱水段。
16. 权利要求15的装置,其中脱水段包括包含蒸气-TEG接触装置的三甘醇脱水段。
17. 权利要求11的装置,其中原料分离器接收冷却到高于水合点的温度的原料气。
18. 权利要求17的装置,其中原料分离器还从原料气中分离出该原料气所含的至少部分水。
19. 权利要求1的装置,包括接收水饱和的C5(+)液体的汽提塔并进一步包含中间塔脱水段,其中该汽提塔作为脱甲烷塔运行,且其中所述汽提塔接收来自中间分离器的回流物,该中间分离器向脱甲烷塔提供C5(+)贫化气体。
20. 权利要求19的装置,其中中间分离器接收在原料气分离器中从原料气分离出的至少一部分脱了水的气体。
21. 权利要求19的装置,其中原料气分离器还制备水饱和的C5(+)液体。
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EA (1) | EA005990B1 (zh) |
MX (1) | MXPA04004256A (zh) |
NO (1) | NO335104B1 (zh) |
WO (1) | WO2003040633A1 (zh) |
Families Citing this family (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20070044485A1 (en) * | 2005-08-26 | 2007-03-01 | George Mahl | Liquid Natural Gas Vaporization Using Warm and Low Temperature Ambient Air |
US20070130991A1 (en) * | 2005-12-14 | 2007-06-14 | Chevron U.S.A. Inc. | Liquefaction of associated gas at moderate conditions |
WO2008002592A2 (en) | 2006-06-27 | 2008-01-03 | Fluor Technologies Corporation | Ethane recovery methods and configurations |
EA013983B1 (ru) * | 2006-07-10 | 2010-08-30 | Флуор Текнолоджиз Корпорейшн | Способ и устройство для кондиционирования газа, обогащенного c5+ углеводородами, и извлечения газоконденсата |
RU2460022C2 (ru) * | 2006-10-24 | 2012-08-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Способ и устройство для обработки потока углеводородов |
GB2473979B (en) * | 2008-07-29 | 2012-09-26 | Shell Int Research | Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream |
US8707730B2 (en) * | 2009-12-07 | 2014-04-29 | Alkane, Llc | Conditioning an ethane-rich stream for storage and transportation |
IT1400370B1 (it) * | 2010-05-31 | 2013-05-31 | Nuova Pignone S R L | Metodo e dispositivo per recuperare gas naturali liquefatti ngl |
US8635885B2 (en) * | 2010-10-15 | 2014-01-28 | Fluor Technologies Corporation | Configurations and methods of heating value control in LNG liquefaction plant |
MY167313A (en) | 2010-10-26 | 2018-08-16 | Kirtikumar Natubhai Patel | Process for separating and recovering ngls from hydrocarbon streams |
US10451344B2 (en) | 2010-12-23 | 2019-10-22 | Fluor Technologies Corporation | Ethane recovery and ethane rejection methods and configurations |
WO2014036322A1 (en) * | 2012-08-30 | 2014-03-06 | Fluor Technologies Corporation | Configurations and methods for offshore ngl recovery |
RU2488428C1 (ru) * | 2012-09-17 | 2013-07-27 | Андрей Владиславович Курочкин | Способ подготовки газа и газового конденсата к транспорту |
CN103351895B (zh) * | 2013-06-07 | 2015-05-06 | 新地能源工程技术有限公司 | 一种页岩气脱水脱重烃的方法及装置 |
BR112017004105B1 (pt) | 2014-09-02 | 2022-10-25 | Ge Oil & Gas, Inc | Métodos para liquefazer e purificar um fluxo de suprimento de etano e um fluxo de etano de alta pressão, e método para refrigerar um fluxo de suprimento de etano |
WO2016130574A1 (en) | 2015-02-09 | 2016-08-18 | Fluor Technologies Corporation | Methods and configuration of an ngl recovery process for low pressure rich feed gas |
US10006701B2 (en) * | 2016-01-05 | 2018-06-26 | Fluor Technologies Corporation | Ethane recovery or ethane rejection operation |
US10330382B2 (en) | 2016-05-18 | 2019-06-25 | Fluor Technologies Corporation | Systems and methods for LNG production with propane and ethane recovery |
CN105854531B (zh) * | 2016-06-17 | 2018-05-01 | 中石化节能环保工程科技有限公司 | 一种密闭式三甘醇脱水系统 |
CA3033088A1 (en) | 2016-09-09 | 2018-03-15 | Fluor Technologies Corporation | Methods and configuration for retrofitting ngl plant for high ethane recovery |
RU175816U1 (ru) * | 2017-05-22 | 2017-12-20 | Акционерное общество "НИПИгазпереработка" (АО "НИПИГАЗ") | Установка извлечения углеводородов с2+выше из нефтяного газа |
US11260342B2 (en) * | 2017-06-15 | 2022-03-01 | Exxonmobil Upstream Research Company | Fractionation system using bundled compact co-current contacting systems |
US11268757B2 (en) * | 2017-09-06 | 2022-03-08 | Linde Engineering North America, Inc. | Methods for providing refrigeration in natural gas liquids recovery plants |
WO2019051101A1 (en) * | 2017-09-07 | 2019-03-14 | Purdue Research Foundation | PROCESS FOR THE VALORISATION OF NATURAL GAS LIQUIDS: A TWO STEP CATALYTIC PROCESS FOR DEHYDROGENATION OF ALKANES AND OLIGOMERISATION |
CA3077409A1 (en) | 2017-10-20 | 2019-04-25 | Fluor Technologies Corporation | Phase implementation of natural gas liquid recovery plants |
FR3088648B1 (fr) * | 2018-11-16 | 2020-12-04 | Technip France | Procede de traitement d'un flux de gaz d'alimentation et installation associee |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4203741A (en) * | 1978-06-14 | 1980-05-20 | Phillips Petroleum Company | Separate feed entry to separator-contactor in gas separation |
US4578094A (en) * | 1983-09-14 | 1986-03-25 | El Paso Hydrocarbons | Hydrocarbon separation with a physical solvent |
CN1292486A (zh) * | 1999-07-01 | 2001-04-25 | 普拉塞尔技术有限公司 | 生产燃料及高纯甲烷的深冷精馏系统 |
US6244070B1 (en) * | 1999-12-03 | 2001-06-12 | Ipsi, L.L.C. | Lean reflux process for high recovery of ethane and heavier components |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4430103A (en) * | 1982-02-24 | 1984-02-07 | Phillips Petroleum Company | Cryogenic recovery of LPG from natural gas |
US4511381A (en) * | 1982-05-03 | 1985-04-16 | El Paso Hydrocarbons Company | Process for extracting natural gas liquids from natural gas streams with physical solvents |
US4743282A (en) * | 1982-05-03 | 1988-05-10 | Advanced Extraction Technologies, Inc. | Selective processing of gases containing olefins by the mehra process |
US4696688A (en) * | 1985-12-13 | 1987-09-29 | Advanced Extraction Technologies, Inc. | Conversion of lean oil absorption process to extraction process for conditioning natural gas |
US4854955A (en) * | 1988-05-17 | 1989-08-08 | Elcor Corporation | Hydrocarbon gas processing |
US5555748A (en) * | 1995-06-07 | 1996-09-17 | Elcor Corporation | Hydrocarbon gas processing |
US5953935A (en) * | 1997-11-04 | 1999-09-21 | Mcdermott Engineers & Constructors (Canada) Ltd. | Ethane recovery process |
US6182469B1 (en) * | 1998-12-01 | 2001-02-06 | Elcor Corporation | Hydrocarbon gas processing |
US6453698B2 (en) * | 2000-04-13 | 2002-09-24 | Ipsi Llc | Flexible reflux process for high NGL recovery |
US6526777B1 (en) * | 2001-04-20 | 2003-03-04 | Elcor Corporation | LNG production in cryogenic natural gas processing plants |
US6742358B2 (en) * | 2001-06-08 | 2004-06-01 | Elkcorp | Natural gas liquefaction |
US6516631B1 (en) * | 2001-08-10 | 2003-02-11 | Mark A. Trebble | Hydrocarbon gas processing |
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Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4203741A (en) * | 1978-06-14 | 1980-05-20 | Phillips Petroleum Company | Separate feed entry to separator-contactor in gas separation |
US4578094A (en) * | 1983-09-14 | 1986-03-25 | El Paso Hydrocarbons | Hydrocarbon separation with a physical solvent |
CN1292486A (zh) * | 1999-07-01 | 2001-04-25 | 普拉塞尔技术有限公司 | 生产燃料及高纯甲烷的深冷精馏系统 |
US6244070B1 (en) * | 1999-12-03 | 2001-06-12 | Ipsi, L.L.C. | Lean reflux process for high recovery of ethane and heavier components |
Also Published As
Publication number | Publication date |
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CA2466167C (en) | 2009-02-10 |
ATE365303T1 (de) | 2007-07-15 |
CN1612998A (zh) | 2005-05-04 |
NO20042304L (no) | 2004-06-03 |
US7051552B2 (en) | 2006-05-30 |
AU2002363532B2 (en) | 2006-04-13 |
CA2466167A1 (en) | 2003-05-15 |
WO2003040633A1 (en) | 2003-05-15 |
EA200400655A1 (ru) | 2004-10-28 |
EP1454103B1 (en) | 2007-06-20 |
MXPA04004256A (es) | 2004-07-08 |
DE60220824T2 (de) | 2008-03-06 |
US20040237580A1 (en) | 2004-12-02 |
EP1454103A1 (en) | 2004-09-08 |
NO335104B1 (no) | 2014-09-15 |
DE60220824D1 (de) | 2007-08-02 |
EA005990B1 (ru) | 2005-08-25 |
EP1454103A4 (en) | 2006-01-11 |
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