CN105492412B - 分离烃气体的方法 - Google Patents
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Abstract
本发明涉及一种将烃气体分离为主要含有甲烷或乙烷以及轻质组分的部分和主要含有C2或C3以及较重组分的部分的方法,其中,进料气体在一个或多个热交换以及膨胀步骤中进行处理;部分冷凝的进料气体被导入分离器,其中,第一残留蒸汽从含有C2或C3的液体中分离;含有C2或C3的液体在基本上分离压力下被导入蒸馏柱,其中,所述液体被分离为第二残留分离以回收含有C2或C3的产物。通过冷却所述第二残留以使其部分冷凝而改进上述方法。
Description
发明背景
本发明涉及一种用于改进从烃气体中回收C2或C3以及较重组分的方法和设备。
在常规的从烃气体中提取乙烷或丙烷以及更重质的成分的方法中,携带C2和/或C3的气体经过膨胀热交换(或压缩之后再膨胀)和制冷的组合处理以获得部分冷凝的气流,该气流收集在通常具有50至1200psia左右的气压和-50°至-200°F左右的温度的进料分离器中。根据使特定气体部分冷凝所必需的压力和温度以及在所述方法中能够进行进料的压力和温度,所述条件可以显著变化。由部分冷凝而得的液体作为中柱供料被注入名为重质分馏柱(HEFC)的分馏柱中,来自供料分离器的蒸汽通过热交换、膨胀或其他方法被进一步冷却,然后作为供料进入轻质分馏柱(LEFC)中。通过适当的热交换方法部分冷凝来自HEFC的顶部蒸汽以使来自LEFC的顶部气流产生回流。在通常的体系中,HEFC柱在低于或基本上相当于HEFC进料分离器(在部分冷凝的液体从分离器到达HEFC的过程中可允许有轻微的压力下降)的压力下运行,HEFC顶部气体在约为0°至-170°F的温度下排出。所述顶部蒸汽针对来自于LEFC的残留蒸汽的热交换提供了作为回流流入LEFC的部分冷凝物。
在膨胀至LEFC压力之前对所述气体的预冷却通常会导致形成高压冷凝物。为避免膨胀器的损坏,如果形成了高压冷凝物,则通常用焦耳-汤姆逊阀使其单独膨胀而分离,并进一步将其供于HEFC柱的中部作为供料使用。在这种方法中的制冷有时完全通过高压气体部分冷凝后至柱运行压力后残留的蒸汽的膨胀做功来产生。其他方法还可包括对高压气体的外部制冷以提供部分所需的冷却。
处理天然气时,通常能够在600-1000psia的管线压力下进行供料。在这种情况下通常会膨胀至约为150-300psia的压力。在一个替代性的方法中,可设计从炼油气中提取乙烷、乙烯、丙烷或丙烯的设备。炼油气通常能够在150psia至250psia的气压下获得。在这种情况下,为了方法设计人的便利,LEFC可设计为在低于可获得的炼油气气压下运行,例如在50-100psia的气压下运行,从而使扩张做功可用于对所述方法提供制冷。这会导致更低的LEFC温度并会增加潜在的热泄露和其他跟低温相关的工程问题。将炼油气压缩至更高的气压以使其之后能够在做功膨胀机器中膨胀来提供整个方法中的制冷,在这种情况下也是可行的。
授予J.古诗比(Jerry G.Gulsby)的美国专利No.4,251,249描述了从气流中分离C3以及更重质的烃的方法的一种常规流程计划。
发明概述
本发明的一个实施方式,描述了一种将至少含有甲烷、乙烷和C3成分的烃气体分离为主要包含乙烷和轻质组分的部分和主要含有C3和较重组分;或主要含有甲烷和轻质组分的部分和主要含有C2和较重组分的部分的方法,所述方法中:
(a)供料气体在一个或多个热交换器以及膨胀步骤中进行处理,以提供至少一种部分冷凝的烃气体,从而提供了至少一种第一残留蒸汽和至少一种含有C2或C3的液体,所述液体还包含轻质烃;
(b)至少一部分含有C2或C3的液体被导入蒸馏柱中,其中,所述液体被分离为含有轻质烃的第二残留和含有C2或C3的产物;包括:
(1)冷却所述第二残留以使其部分冷凝;
(2)使一种所述第一残留蒸汽中的至少一部分与所述部分冷凝的第二残留的液体部分的至少一部分在至少一个接触阶段充分接触,接着在所述接触阶段中将蒸汽和液体进行分离;
(3)将回收的液体作为液体供料供入蒸馏柱中;
(4)导入回收的蒸汽使其与所述来自蒸馏柱的第二残留进行热交换,从而提供步骤(1)的冷却,之后排放所述残留气体;所述改进还进一步包括:
(5)从膨胀器-压缩器或残留气体压缩器中回收一种再循环气流;
(6)在所述一个或多个热交换器中冷却并部分冷凝所述再循环气流;
(7)使所述再循环气流膨胀从而进一步冷凝一部分再循环气流并使之冷却;
(8)将膨胀的再循环气流供入过冷器中,所述膨胀的再循环气流与来自重质分馏柱顶部的气体在过冷器中进行热交换,向来自重质分馏柱的蒸汽提供更冷的温度。
所述接触步骤(2)在供料分离器/收集器中进行,所述供料分离器/收集器包括用于蒸汽/液体逆流接触的分馏装置,其中
(i)所述部分冷凝的第二残留被导入所述分馏装置的中间点或上部的所述分离器/收集器,其液体部分在所述分馏装置中向下流动;
(i i)所述第一残留的部分冷凝的部分被导入所述分馏装置中间点或上部的所述分离器/收集器,其液体部分在所述分馏装置中向下流动;其中,所述被冷却的含有C2或C3的来自分离器的液体的一部分被导入所述分馏装置上部或中间点的所述分离器/收集器,其液体部分在所述分馏装置中向下流动;
(i i i)一种所述第一残留蒸汽的至少一部分被导入所述分馏装置下部的所述分离器/收集器,第一残留蒸汽与部分冷凝的第二残留的液体部分逆流接触,在所述分馏装置中上升。
在所述分离器/收集器中的分馏装置提供与至少一种理论蒸馏阶段相当的阶段,该阶段使一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分相接触。
在所述分离器/收集器中的分馏装置提供与至少一种理论蒸馏阶段相当的阶段,该阶段使一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分相接触。
回收的再循环气流,在一个或多个热交换器中部分冷凝之前可进一步通过膨胀器-压缩器排放冷却器或其他压缩排放冷却器。所述将再循环气流部分冷凝的一个或多个热交换器,能够使除来自轻质分馏柱顶部的气体以外的其他液体和气流流通,以进一步用来部分冷凝再循环气流。例如,来自轻质分馏柱的液态产物-重沸流体、侧部加热器流体和/或残留气流可全部通过一个或多个热交换器。
所述一个或多个热交换器可以是壳式和管式、板翅式热交换器,或者是其他类型的热交换器。所述再循环气流的膨胀可通过流经流量控制阀或附加的涡轮膨胀器来实现。
供入过冷器的冷胀再循环气流与来自轻质分馏柱的顶部气流组合而产生被供入轻质分馏柱的更冷的回流,从而促进增强的回流,因此从轻质分馏柱能够更好地进行回收。
进一步描述了一种将至少含有乙烷和C3成分的烃气体分离为主要包含乙烷和轻质组分的部分和主要包含C3和较重组分的部分的装置,所述装置中
(a)提供相互协同连接的一种或多种热交换装置以及一种或多种膨胀装置,以提供至少一种部分冷凝的烃气体,从而提供至少一种第一残留蒸汽和至少一种含有C3和轻质烃的液体,
(b)连接一个蒸馏柱以接收至少一种所述含有C3的液体,所述蒸馏柱经过调整以将含有C3的液体分离为包含轻质烃的第二残留和包含C3的产物,改进包括:
(1)与所述蒸馏柱相连的热交换装置,用以接收所述第二残留并使之部分冷凝;
(2)与所述蒸馏柱相连的接触和分离装置,用以接收一种第一残留蒸汽的至少一部分和部分冷凝的第二残留的液体部分的至少一部分,还用以在至少一个接触阶段混合所述蒸汽和液体,该装置包含在所述阶段中接触之后将蒸汽和液体分离的分离装置;
(3)所述装置(2)进一步相连以提供被分离而进入蒸馏柱的作为液体供料的液体,
(4)所述装置(2)也相连以将被分离的蒸汽导入而与所述热交换装置(1)中的来自蒸馏柱的所述第二残留进行热交换;改进还包括
(5)与所述蒸馏柱相连的产物冷却器装置,用以接收来自所述蒸馏柱的所述第二残留并将所述第二残留供入所述热交换装置中。
该接触和分离装置包括用于逆流蒸汽/液体接触的分馏装置,其中所述装置连接以接收要在所述分馏装置下部处理的一种第一残留蒸汽的一部分,还用以接收来自在所述装置上部经过处理的部分冷凝的第二残留的所述液体的一部分,所述分馏装置经过调整从而该第一残留蒸汽上升并与部分冷凝的第二残留以逆流的形式接触。
所述分馏装置包括蒸汽/液体接触装置,该装置与至少一种理论蒸馏阶段相当。
所述接触与分离装置(2)包括将一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分进行混合的装置。
所述接触与分离装置(2)包括将一种所述第一残留蒸汽的至少一部分与所述部分冷凝的第二残留的液体和蒸汽部分进行混合的装置。
所述接触和分离装置包括用于逆流蒸汽/液体接触的装置,其中所述装置相连以接收以下部分:在所述分馏装置下部处理的一种第一残留蒸汽;来自部分冷凝的第二残留的所述液体;部分冷凝的第一残留;来自分离器的在所述分馏装置的上部或中间点处理的被冷却的含有C3的液体,所述分馏装置经过调整从而该第一残留蒸汽上升并与部分冷凝的第二残留以逆流的形式接触;部分冷凝的第一残留,该装置经过进一步调整从而来自分离器的含有C3的液体被分馏装置排出的液体冷却。
所述分馏装置包括蒸汽/液体接触装置,该接触装置与至少一种理论蒸馏阶段相当。
所述接触与分离装置(2)包括将一种所述第一残留蒸汽的至少一部分与以下部分混合的装置:部分冷凝的第二残留的液体部分;第一残留的部分冷凝的部分的液体部分;部分来自分离器的被冷却的含有C3的液体。
所述接触与分离装置(2)包括将一种所述第一残留蒸汽的至少一部分与以下部分混合的装置:所述部分冷凝的第二残留的液体和蒸汽部分;所述第一残留的部分冷凝的部分;部分来自分离器的被冷却的含有C3的液体。
附图简述
图1A是基于本发明的烃分离方法的部分示意图,因缩放限制本图只示出一半的方法。
图1B是基于本发明的烃分离方法的另一部分示意图,因缩放限制本图只示出另一半的方法。
发明描述
本发明提供一种得到改进的用于从携带烃的气体中回收C2或C3以及更重质的成分的方法。在本发明改进的方法中,来自HEFC柱的顶部蒸汽被部分冷凝,液体冷凝物至少与来自如上所述的部分冷凝的供料气体的至少蒸汽部分在LEFC中组合,在部分发明中,所述LEFC也作为收集器。该LEFC被设计为能够提供一个或多个接触阶段。通常假定这类阶段用于平衡阶段的设计用途,但在实际情况中并不必如此。来自供料分离器/收集器的蒸汽与来自HEFC的顶部气流进行热交换,从而使该气流部分冷凝,来自LEFC的液体作为上部或顶部液体供料被供于HEFC柱。
若LEFC包含一个吸收段,例如填料,或者一个或多个分馏塔板,则假定这些阶段与合适数量的理论分离阶段相应。本发明者的计算显示,在少至一种理论阶段时也具有优势,理论阶段数量增加则具有更大的优势。本发明者相信即使仅有一个与分离理论阶段相当的阶段也能实现该优势。该部分冷凝的HEFC顶部气流被供于该吸收段之上,其液体部分向下流过该吸收段。所述部分冷凝的供料气流通常被供于该吸收段之下,从而其蒸汽部分向上穿过该吸收段,以逆流的形式与来自部分冷凝的HEFC顶部气流的液体接触。所述上升蒸汽与来自吸收段之上的部分冷凝的HEFC顶部气流的蒸汽组合,以形成组合残留气流。
虽然以上对将顶部蒸汽冷凝并用于从膨胀器释放的蒸汽中吸收有价值的乙烷、乙烯、丙烷、丙烯等的优选实施方式进行了描述,但是本发明者指出本发明并不仅限于这一具体实施方式。所述优势可通过下述方式实现,例如仅以这种方式处理一部分膨胀器释放的蒸汽,或者在其他设计考虑指出膨胀器释放的蒸汽和顶部冷凝物应该绕过LEFC的情况下,仅使用部分顶部冷凝物作为吸收剂。本发明者还指出能够以分离容器或HEFC柱的一个部分的形式来构建LEFC。
本发明实践中,在LEFC和HEFC之间必然会有轻微的压力差,该压力差必须予以考虑。如果顶部蒸汽穿过冷凝器并进入分离器,而未产生任何压力的上升,则假定LEFC的运行压力稍微低于HEFC的运行压力。在这种情况下,从LEFC排出的液体供料能够被泵入HEFC的供料位置。一种替代性方案是在蒸汽管线中提供一个升压鼓风机,以有效提高顶部冷凝器和LEFC的运行压力,从而液体供料可以在不泵送的情况下被供入HEFC。另外一种替代性方案是在相对于从LEFC排出的液体的供料位置足够高的位置安装LEFC,从而液体的静压头会克服压力差。
在另外一种替代性方案中,全部或部分的部分冷凝HEFC顶部气流以及全部或部分的部分冷凝供料可以组合,例如在管线中与膨胀器排出的成分组合而输出至LEFC,如果充分混合,则液体和蒸汽会一起混合并根据全部组合气流中不同组分的相对挥发性而分离。在该实施方式中,来自顶部冷凝器的蒸汽-液体混合物可以不经分离而使用,或者可将其液态粉末进行分离。认为这种混合的目的是在本发明中作为接触阶段。
在所述方案的一种变化形式中,部分冷凝的顶部蒸汽可被分离,整体或部分被分离的液体被供于LEFC或者与被供入的蒸汽混合。
本发明提供了一种在运行所述方法所需的单位功率输入下乙烷、乙烯、丙烷或丙烯的回收得到了改进的方法。对运行HEFC方法所需的运行功率的改进可体现在外部制冷所需功率的降低,或者是压缩或再压缩所需功率的降低,或者是两种功率均降低。或者,在需要时可通过固定的功率输入来实现C2或C3回收量的增加。
图1A和图1B表示基于本发明的烃分离方法的示意图。携带烃的天然气经过管线20被供入热气/气体交换器22-E3000,然后到达冷却装置22-E3400。通过管线52和53来提供制冷。冷却装置具有管线54,该管线撤回用于再压缩和液化的制冷。该冷却气流通过管线21经过一个冷气/气体交换器22-3100被供入冷分离容器22-D1000。
该烃气流将会被分离为两股气流,蒸汽通过管线22离开容器,底部气流通过管线25到达管线16。底部残留将会流经管线26上用于控制流量的阀门,然后重新回到管线26并到达管线35,经管线35将会进入过冷器22-E3200。这些冷却烃气体经管线36离开过冷器,然后进入轻质分馏柱22-T2000。未转移的烃气流会继续经过管线37到达轻质分馏柱22-T2000的柱的顶部。
来自冷分离容器22-D1000的蒸汽会经管线22离开,然后到达与管线24的交叉点。管线24还包含一个阀门组件PV,该组件用于控制管线24中的流量。来自冷分离容器的剩余蒸汽流经管线23并穿过膨胀器/压缩器22-X6000。该膨胀烃气流经管线29被供入轻质分馏柱22-T2000。
来自轻质分馏柱22-T2000的蒸汽通过管线39离开并流经管线40,在此,它们经过冷气/气体交换器22-E3100和热气/气体交换器,然后经管线55到达压缩气流将会进入的膨胀器/压缩器22-C6000,在此,压缩的气流经管线59到达膨胀器/压缩器排气冷却器22-E4100。排放气流会经管线58排出,根据需要用于销售或进一步处理。
管线56与管线55连接,在进入膨胀器/压缩器22-C6000之前,部分烃气体会被抽出并回收用作燃气。一个阀门组件安装于管线56上以控制将作为燃气使用的气体的量。
来自轻质分馏柱22-T2000的底部残留会经管线31排出。这些底部残留物包括需要进一步分馏的中间体液流。管线31向输送泵22-P5000A/B输入流动液体,输送泵将来自轻质分馏柱的底部残留物导入管线33并进入重质分馏柱22-T2100的顶部。
含有更冷的中间产物的液流经管线41从重质分馏柱22-T2100抽出,然后供入侧部加热器22-E3800,该加热器加热该液流并通过管线42将其供回比抽出该液流的重质分馏柱上的部位更低的部位。另外一股副产物液流经管线43从重质分馏柱22-T2100抽出并被供入重质分馏柱的重沸器22-E3700,该重沸器将加热该副产物液流。该液流被供入调温重沸器22-E4000,在其中被进一步加热,然后经管线44被供回比抽出该液流的重质分馏柱上的部位更低的部位。管线45向调温重沸器22-E4000提供加热介质(图中未显示),管线46从调温重沸器中将加热介质供回。
位于重质分馏柱底部的一条管线会将部分主要含有C2和更少量挥发性烃或主要含有C3和更少量挥发性烃的烃移除并导入管线51上的阀门。管线51接收来自重质分馏柱22-T2100的底部残留物。管线47将来自重质分馏柱的底部残留物供入重质分馏柱的底部残留物泵22-P5100A/B中,该泵经管线49将底部残留物供入产物交换器22-E3600,该交换器经管线50将底部残留物供入产物泵22-P5200A/B。该泵通过管线51将底部残留物导出,所述管线51可将底部残留物直接供料于管线中。管线49上的阀门能够绕过产物交换器22-E3600并在设备处于C3和更重质烃回收模式的情况下将残留物导入气冷或水冷热交换器中。冷却之后,这些底部残留物可通过管线49被供回产物交换器22-E3600。
来自重质分馏柱22-T2100的蒸汽经管线34排出并穿过过冷器22-E3200。管线38连接过冷器22-E3200的排出口和阀门。来自重质分馏柱的蒸汽经管线30被供入轻质分馏柱22-T2000,其中蒸汽会被进一步分馏以作为回流再次进入重质分馏柱。
部分来自气流58的被压缩的残留气体通过整个的低温方法被回收,目的不仅在于增加乙烷和更重质的烃组分的回收,也在于减少整个***的能量消耗。
所述得到改进的方法利用再循环气流1,其中部分残留气体被冷却并可通过热交换部分液化,然后膨胀,降低其温度从而增加轻质分馏柱22-T2000中的回流。该再循环气流1从膨胀器-压缩器22-X/C600和膨胀器-压缩器排气冷却器22-E4100向下供料,或者通过残留气体压缩器后冷却器向下供料。该再循环气流1在输入板翅型热交换器22-E3000中被冷却并部分冷凝,其中该再循环气流1可与输入气流20、液态产物流49、重沸器流体流43、侧部加热器气流体流41和残留气流40共同进行交叉交换。该再循环气流经管线2排出热交换器22-E3000并通过流量控制阀V2进行膨胀,其中,会对再循环气流产生进一步的液化和冷却。所述被进一步冷却和液化的再循环气流穿过流量控制阀V2并进入管线3,被供入过冷器22-E3200。过冷器22-E3200通过混合来自轻质分馏柱22-T2000的蒸汽来提供额外的制冷。通过达到所述低温会产生额外的液化,从而向轻质分馏柱22-T2000提供更多的回流。所述回流会导致更多的乙烷吸附,也会增加乙烷和较重组分的回收。
所述向过冷器22-E3200提供了更多冷却并进一步向轻质分馏柱22-T2000提供更冷的回流的再循环气流穿过过冷器22-E3200并进入管线4,其中,该再循环气流到达管线40并通过热交换器22-E3000被供入,在热交换器22-3000中该再循环气流被进一步加热然后通过管线55被供入膨胀器/压缩器22-C6000。所述被压缩的气流将通过管线59被供入膨胀器/压缩器排气冷却器22-E4100,其中,该气流将被再次压缩并供入管线1,在管线1中所述气流最终将被回收至过冷器22-E3200。
虽然关于本发明的具体实施方式描述了本发明,但是显然,本发明的许多其他形式和改变对本领域技术人员是显而易见的。本发明所附的权利要求书一般应被解释成包括在本发明的真正精神和范围之内的所有这些显而易见的形式和改变。
Claims (24)
1.一种将至少含有乙烷和C3以及较重组分的烃气体分离为主要包含乙烷和轻质组分的部分和主要包含C3和较重组分的部分的方法,其特征在于,所述方法中
(a)所述烃气体在一个或多个热交换器以及膨胀步骤中进行处理,以提供至少一种部分冷凝的烃气体,从而提供了至少一种第一残留蒸汽和至少一种含有C2或C3的液体,所述液体还包含轻质烃;
(b)至少一种含有C2或C3的液体被导入蒸馏柱中,其中,所述液体被分离为含有轻质烃的第二残留和含有C2或C3的产物;
所述改进包括:
(1)冷却所述第二残留以使其部分冷凝;
(2)使一种所述第一残留蒸汽中的至少一部分与所述部分冷凝的第二残留的液体部分中的至少一部分在至少一个接触阶段中充分接触,接着在所述接触阶段中将蒸汽和液体进行分离;
(3)将在所述接触阶段中分离得到的液体作为液体供料供入蒸馏柱中;
(4)导入在所述接触阶段中分离得到的蒸汽使其与所述来自蒸馏柱的第二残留进行热交换,从而提供步骤(1)的冷却,之后排放残留气体;
所述改进还进一步包括:
(5)从膨胀器-压缩器或残留气体压缩器中回收再循环气流;
(6)在所述一个或多个热交换器中冷却并部分冷凝所述再循环气流;
(7)使所述再循环气流膨胀从而进一步冷凝一部分再循环气流并使之冷却;
(8)将膨胀的再循环气流供入过冷器中,所述膨胀的再循环气流与来自蒸馏柱顶部的气体在过冷器中进行热交换;向来自蒸馏柱的第二残留提供更冷的温度。
2.如权利要求1所述的方法,其中,所述接触步骤(2)在轻质分馏柱中进行,所述轻质分馏柱包括用于蒸汽/液体逆流接触的分馏装置,其中
(ⅰ)所述部分冷凝的第二残留被导入所述分馏装置上的轻质分馏柱中,其液体部分在所述分馏装置中向下流动;
(ⅱ)一种所述第一残留蒸汽的至少一部分被供入所述分馏装置下的轻质分馏柱中,第一残留蒸汽与部分冷凝的第二残留的液体部分逆流接触,在所述分馏装置中上升。
3.如权利要求2所述的方法,其特征在于,在所述轻质分馏柱中的分馏装置提供与至少一种理论蒸馏阶段相当的阶段,该阶段使一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分相接触。
4.如权利要求1所述的方法,其特征在于,一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分进行共混合。
5.如权利要求1所述的方法,其特征在于,一种所述第一残留蒸汽的至少一部分与所述部分冷凝的第二残留的液体部分和蒸汽部分进行共混合。
6.如权利要求1所述的方法,其特征在于,通过向来自蒸馏柱的第二残留提供更冷的温度提高了来自轻质分馏柱的乙烷和较重组分的产率。
7.如权利要求1所述的方法,其特征在于,在所述一个或多个热交换器中冷凝之前,所述已回收的再循环气流被进一步供入膨胀器/压缩器排放冷却器或残留气体压缩器排放冷却器中。
8.如权利要求1所述的方法,其特征在于,所述一个或多个热交换器接收额外的气流和液流以冷却并部分冷凝所述再循环气流。
9.如权利要求7所述的方法,其特征在于,所述额外的气流和液流选自进口气流、液态产物流、重沸器流体流、侧部加热器流体流、制冷剂流和残留气流。
10.如权利要求1所述的方法,其特征在于,所述一个或多个热交换器为板翅热交换器、壳式和管式热交换器或绕线式热交换器。
11.如权利要求1所述的方法,其特征在于,使所述再循环气流膨胀是通过流量控制阀或涡轮膨胀器进行。
12.如权利要求1所述的方法,其特征在于,冷却的所述再循环气流来自蒸馏柱。
13.一种将至少含有甲烷和C2以及较重组分的烃气体分离为主要包含甲烷和轻质组分的部分和主要包含C2和较重组分的部分的方法,其特征在于,所述方法中
(a)烃气体在一个或多个热交换器以及膨胀步骤中进行处理,以提供至少一种部分冷凝的烃气体,从而提供了至少一种第一残留蒸汽和至少一种含有C2的液体,所述液体还包含轻质烃;
(b)至少有一种含有C2的液体被导入蒸馏柱中,其中,所述液体被分离为含有轻质烃的第二残留和含有C2的产物;
改进包括:
(1)冷却所述第二残留以使其部分冷凝;
(2)使一种所述第一残留蒸汽中的至少一部分与部分冷凝的第二残留的液体部分中的至少一部分在至少一个接触阶段中充分接触,接着在所述接触阶段中将蒸汽和液体进行分离;
(3)将在所述接触阶段中分离得到的液体作为液体供料供入蒸馏柱中;
(4)导入在所述接触阶段中分离得到的蒸汽使其与所述来自蒸馏柱的第二残留进行热交换,从而提供了步骤(1)的冷却,之后排放残留气体;所述改进还进一步包括:
(5)从膨胀器-压缩器或残留气体压缩器中回收再循环气流;
(6)在所述一个或多个热交换器中冷却并部分冷凝再循环气流;
(7)使所述再循环气流膨胀从而进一步冷凝一部分再循环气流并使之冷却;
(8)将膨胀的再循环气流供入过冷器中,所述膨胀的再循环气流与来自蒸馏柱顶部的气体在过冷器中进行热交换,向来自蒸馏柱的第二残留提供更冷的温度。
14.如权利要求13所述的方法,其中,所述接触步骤(2)在轻质分馏柱中进行,所述轻质分馏柱包括用于蒸汽/液体逆流接触的分馏装置,其中
(ⅰ)所述部分冷凝的第二残留被导入所述分馏装置上的轻质分馏柱中,其液体部分在所述分馏装置中向下流动;
(ⅱ)一种所述第一残留蒸汽的所述至少一部分被供入所述分馏装置下的轻质分馏柱中,第一残留蒸汽与部分冷凝的第二残留的液体部分逆流接触,在所述分馏装置中上升。
15.如权利要求13所述的方法,其特征在于,在所述轻质分馏柱中的分馏装置提供与至少一种理论蒸馏阶段相当的阶段,该阶段使一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分相接触。
16.如权利要求13所述的方法,其特征在于,一种所述第一残留蒸汽的至少一部分与部分冷凝的第二残留的液体部分进行共混合。
17.如权利要求13所述的方法,其特征在于,一种所述第一残留蒸汽的至少一部分与所述部分冷凝的第二残留的液体部分和蒸汽部分进行共混合。
18.如权利要求13所述的方法,其特征在于,通过向来自蒸馏柱的第二残留提供更冷的温度提高了来自轻质分馏柱的乙烷和较重组分的产率。
19.如权利要求13所述的方法,其特征在于,在所述一个或多个热交换器中冷凝之前,所述已回收的再循环气流被进一步供入膨胀器/压缩器排放冷却器或残留气体压缩器排放冷却器。
20.如权利要求13所述的方法,其特征在于,所述一个或多个热交换器接收额外的气流和液流以冷却并部分冷凝所述再循环气流。
21.如权利要求20所述的方法,其特征在于,所述额外的气流和液流选自进口气流、液态产物流、重沸器流体流、侧部加热器流体流、制冷剂流和残留气流。
22.如权利要求13所述的方法,其特征在于,所述一个或多个热交换器为板翅热交换器、壳式和管式热交换器或绕线式热交换器。
23.如权利要求13所述的方法,其特征在于,使所述再循环气流膨胀是通过流量控制阀或涡轮膨胀器进行。
24.如权利要求13所述的方法,其特征在于,冷却的所述再循环气流来自蒸馏柱。
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US9581385B2 (en) | 2017-02-28 |
AU2014265950A1 (en) | 2015-11-19 |
BR112015028448A2 (pt) | 2017-07-25 |
RU2015153401A (ru) | 2017-06-22 |
RU2658010C2 (ru) | 2018-06-19 |
US20140338396A1 (en) | 2014-11-20 |
BR112015028448B1 (pt) | 2021-03-09 |
CN105492412A (zh) | 2016-04-13 |
EP2997001A1 (en) | 2016-03-23 |
CA2912171C (en) | 2021-10-19 |
AU2014265950B2 (en) | 2018-12-20 |
EP2997001A4 (en) | 2017-04-19 |
CA2912171A1 (en) | 2014-11-20 |
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