CN103857648B - 改造天然气加工液态产物回收成套设备的构造和方法 - Google Patents

改造天然气加工液态产物回收成套设备的构造和方法 Download PDF

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CN103857648B
CN103857648B CN201280040654.6A CN201280040654A CN103857648B CN 103857648 B CN103857648 B CN 103857648B CN 201280040654 A CN201280040654 A CN 201280040654A CN 103857648 B CN103857648 B CN 103857648B
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interchanger
resorber
feed gas
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J.马克
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Abstract

本发明涉及改造天然气加工液态产物成套设备以将从各种进料气体中回收C3+烃扩展到回收C2+和C3+烃的装置和方法。在特别优选的方面，集成专用的C2+交换器以排他地冷却进料气体以生成冷却的吸收器进料并且生成两个单独的吸收器回流物流。在C2+回收期间，吸收器回流由一部分残余气体和一部分所述进料气体提供，而在C3+回收期间，吸收器和蒸馏塔回流由蒸馏塔塔顶产物提供。

Description

改造天然气加工液态产物回收成套设备的构造和方法
本申请要求序号61/499033的我们同时待审的美国临时专利申请的优先权，该专利申请在2011年6月20日提交，其通过引用结合到本文中来。
发明领域
本发明的领域为天然气加工，特别地讲，本发明涉及改造天然气加工液态产物(natual gas liguid, NGL)成套设备以从丙烷回收操作到乙烷回收操作。
发明背景
大多数天然气成套设备设计成调节进料气体以满足管线售气规格(例如，需要特定的烃露点和水含量)，其通常通过提取丙烷+组分来实现。气体成套设备操作的主要收入由冷凝组分的销售产生，这些冷凝组分主要为丙烷、丁烷和更重的烃。因此，大部分所述成套设备构造成使丙烷回收率最大化。过去，在进料气体中的乙烷含量仅由于其热含量而有价值，且没有回收乙烷的显著动机。然而，随着对于使用乙烷作为原料的石化设施的要求逐渐增加，乙烷可以高价出售。设计用于传统回收丙烷的气体成套设备现在考虑回收乙烷操作。然而，改造现有设施来制造乙烷产物通常困难且成本高。
在本领域中已知从天然气中分馏NGL馏分的许多分离方法和构造。在典型的气体分离方法中，高压进料气流通过在大多数情况下使用丙烷冷冻和涡轮膨胀的换热器冷却，其冷却程度取决于进料气体的富集程度和所要的回收率水平。因为进料气体在加压下冷却，所以烃液被冷凝且与冷却的气体分离。随后使该液体膨胀并在蒸馏塔(例如，脱乙烷塔或脱甲烷塔)中分馏以将诸如甲烷、氮气和其他轻组分的较轻组分作为塔顶蒸气与NGL塔底产物分离。
例如，Rambo等在美国专利5,890,378号中描述了其中吸收器回流的系统，其中脱乙烷塔冷凝器提供吸收器和脱乙烷塔两者的回流，同时冷却任务由涡轮膨胀和丙烷制冷供应。在此，吸收器和脱乙烷塔在基本相同的压力下操作。虽然Rambo的构造常可通过额外设备来产生回流而有效地回收98%的C3+烃，但特别是在进料气体压力低(例如，小于600psig)时，高乙烷回收率(例如，超过80%)变得困难。高乙烷回收率通常需要降低吸收器压力，这继而增加了再压缩马力需求。遗憾的是，较低的压力还增加了在脱甲烷塔中的CO2冻结温度，尤其是在进料气体含有显著量的CO2时。
为了智取至少一些与相对较低的效率和回收率相关的问题，Sorensen在美国专利5,953,935号中公开了一种成套设备构造，其中吸收器回流通过除了使另一部分进料气体膨胀之外还使进料气体的滑流冷却并焦耳-汤姆逊(Joule-Thomson)膨胀来生成。虽然Sorensen的构造可实现高乙烷回收率，但其仅可适用于非常贫乏的气体，同时需要脱甲烷塔在极低的压力下操作，这再一次需要额外的残余气体再压缩功率。
在其他已知的构造中，用各种改善的分馏和回流构造来尝试高NGL回收率。典型的实例公开在Campbell等的美国专利4,278,457号和美国专利4,854,955号、Elliott等的美国专利6,244,070号和Foglietta的美国专利5,890,377号中。虽然这类构造可提供优于现有方法的至少一些优势，但它们通常旨在以固定的回收模式：乙烷回收或丙烷回收操作。此外，这类已知构造中的大多数在成套设备从丙烷回收变到乙烷回收时或者反过来时需要彻底改进涡轮膨胀机并改变操作条件。在大多数情况下，乙烷回收率限于20%-40%，而较高的乙烷回收率将需要过大的再压缩功率且将产生较低的丙烷回收率。
为了智取至少一些与高乙烷回收率相关的问题，同时维持高丙烷回收率，双回流法(描述在Mak等的美国专利7,051,553号中)采用其中第一塔接收两个回流物流的构造：一个回流物流包含NGL的蒸气部分且另一回流物流包含由第二蒸馏塔的塔顶馏分提供的贫乏回流。类似地，Mak等的美国专利申请2010/0206003号描述了改进的天然气加工液态产物回收方法，其中将残余气体集成到丙烷回收设计中，使得其可在高乙烷回收率期间用于回流脱甲烷塔。虽然这些方法可对于丙烷回收或乙烷回收操作，但所述构造通常仅适合基层安装(grass root installation)，而不适合改造。此外，使用这类方法仍然没有灵活地、也没有经济地实现很高的乙烷回收率(例如，超过90%)。本文中的所有出版物都通过引用结合到本文中，其引用的程度就如同具体且单个地指出将各个出版物或专利申请通过引用结合到本文中一样。在所结合的参考文献中的术语的定义或使用与本文提供的术语的定义不一致或相反的情况下，本文提供的术语的定义适用，而参考文献中的术语的定义不适用。
因此，尽管已知回收天然气加工液态产物的各种构造和方法，但其所有或几乎所有都受到一个或多个缺点困扰。例如，虽然可采用一些已知方法和构造用于丙烷回收和乙烷回收两者，但这类成套设备的资金和操作成本可能很高且可能不合理。另一方面，改造现有丙烷回收成套设备以用于乙烷回收需要显著较少的投资。然而，改造需要根据成套设备的构造和操作采取完全不同的对策。因此，需要提供改造丙烷回收成套设备以用于乙烷回收的方法和构造，特别是在需要超过90%的高乙烷回收率的情况下。
发明概述
本发明涉及用于改造双塔式NGL回收成套设备的方法和套装，其中吸收器接收由专用换热器提供的交替回流物流。对于C3+回收(即，丙烷和更高级烃的回收)，所述回流为来自蒸馏塔的塔顶液体，且对于C2+回收(即，乙烷和更高级烃的回收)，将两种单独的回流物流进料到所述吸收器中，其中第一回流物流由一部分残余气体形成且第二回流物流由一部分进料气体形成。在特别优选的方面，改造的成套设备允许至少90%的C2回收率和至少99%的C3+回收率，其中C2回收率具有从2%到98%的灵活性，同时维持99%或更高的C3+回收率。
所涉及的成套设备、套装和方法特别适合改造现有的C3+回收成套设备以允许高C2回收率，同时保留原始的C3+回收成套设备部件和操作方案。因此，应该认识到，当仅需要回收C3+时，可使用所涉及的成套设备和方法来拒绝C2，并且操作的改变可通过程控切换阀自动操作。
在本发明主题的一方面，涉及改造天然气加工液态产物成套设备以便回收C2+烃的方法，其中所述NGL成套设备具有吸收器、下游蒸馏塔和构造成冷却进料气体并冷却来自所述蒸馏塔的塔顶产物以由此形成用于所述吸收器的回流物流的C3+回收交换器，且其中将所述吸收器的塔底产物进料到所述下游蒸馏塔。在这类方法中，特别优选安装用于所述C3+回收交换器的旁通管路，所述旁通管路包括第一专用C2+回收交换器和第二专用C2+回收交换器。最典型地，所述第一C2+回收交换器使用来自吸收器塔顶产物的制冷容量以由一部分压缩的残余气体生成超贫乏回流物流并由所述进料气体的一部分生成回流物流，且所述第二C2+回收交换器使用来自所述吸收器塔底产物的制冷容量以由所述进料气体的另一部分生成冷却的进料气体。在另一步骤中，安装将来自所述蒸馏塔的塔顶产物作为汽提蒸气导引到所述吸收器的旁路。
在所涉及的这类方法的又一优选的方面，安装将所述冷却的进料气体的液体部分提供到所述吸收器的管路，和/或安装控制切换阀的操作以在需要回收C2+时流体绕过所述C3+回收交换器的控制管路。通常更优选的是使用所述蒸馏塔的塔顶冷凝器以生成冷却的进料气体。同样，优选在将所述冷却的进料气体的蒸气部分进料到所述吸收器中之前使所述蒸气部分膨胀到吸收器的压力。
因此，从不同的观点来考虑，涉及改造天然气加工液态产物成套设备以便回收C2+烃的方法和套装。在这类方法中，所述天然气加工液态产物成套设备具有吸收器、下游蒸馏塔和构造成冷却进料气体并冷却来自所述蒸馏塔的塔顶产物以由此形成用于所述吸收器的回流物流的C3+回收交换器，且其中将所述吸收器的塔底产物进料到所述下游蒸馏塔。
在特别优选的方法中，安装第一专用C2+回收交换器和第二专用C2+回收交换器、管道和多个切换阀，使得：(a) 所述进料气体流排他地导引到所述C3+回收交换器或所述第一C2+回收交换器和所述第二C2+回收交换器，其中所述C3+回收交换器构造成由所述进料气体生成冷却的进料气体，其中所述第一C2+回收交换器构造成由所述进料气体的第一部分生成进料气体回流物流，且其中所述第二C2+回收交换器构造成由所述进料气体的第二部分生成冷却的进料气体；(b) 所述吸收器的塔底产物流排他地导引到所述C3+回收交换器或所述第二C2+回收交换器以将制冷容量提供到所述C3+回收交换器或所述第二C2+回收交换器；(c) 所述吸收器的塔顶产物流排他地导引到所述第一C2+回收交换器以提供制冷容量，从而由一部分压缩的残余气体产生用于所述吸收器的超贫乏回流物流；和(d) 所述蒸馏塔的塔顶产物流可作为汽提蒸气排他地导引到所述吸收器或作为用于所述吸收器的回流物流排他地导引到所述吸收器和作为蒸馏塔回流排他地导引到所述蒸馏塔。
在其他特别优选的方面，所述切换阀中的至少一个为三通阀，且更通常优选安装控制所述切换阀的操作以在需要回收C2+时绕过所述C3+回收交换器的控制管路。虽然并未限制本发明的主题，但还是优选所述蒸馏塔的塔顶冷凝器与所述第二C2+回收交换器流体连接以由所述进料气体的第二部分生成冷却的进料气体。
本发明的各种目的、特点、方面和优势从本发明的优选实施方案的以下详述将变得更加显而易见。
附图简述
图1为根据本发明主题的改造用于乙烷回收的一种示例性丙烷回收成套设备的示意图。
图2为根据本发明的主题在乙烷回收操作期间图1的乙烷回收交换器(57)的复合热曲线(composite heat curve)。
发明详述
本发明人已经发现，可改造双塔式NGL回收成套设备(即，具有吸收器和流体连接的下游蒸馏塔的成套设备)以使得从进料气体中回收C3+可以概念上简单且有效的方式扩展到回收C2+。在特别优选的方法和系统中，改进所述成套设备以使得所述吸收器从专用换热器接收交替回流物流且使用来自不同来源的回流物流。
对于C3+回收(即，丙烷和更高级烃的回收)，所述回流为来自蒸馏塔的塔顶液体，且对于C2+回收(即，乙烷和更高级烃的回收)，将两种单独的回流物流进料到所述吸收器中，其中第一回流物流由一部分残余气体形成且第二回流物流由一部分进料气体形成。在特别优选的方面，改造的成套设备允许至少90%的C2回收率和至少99%的C3+回收率，其中C2回收率具有从2%到98%的灵活性，同时维持99%或更高的C3+回收率。从另一观点考虑，使用专门回收C2+和回收C3+的回收交换器的成套设备和方法在C2+回收操作期间将实现超过90%的乙烷回收率，同时维持99.5%的丙烷回收率，且在C3+回收(C2拒绝)操作期间将实现相同的丙烷回收率。
特别考虑的回收交换器包括构造成由残余气体和一部分进料气体生成冷冻的回流物流的C2+回收交换器，和构造成由第二分馏(蒸馏)塔形成回流的C3+回收交换器。因为所考虑的系统和方法不需要对现有C3+回收成套设备进行任何实质性改进，所以改造特别简单，同时维持现有成套设备的所要的C3+回收率。应该进一步认识到可使用所考虑的成套设备和方法以在仅需要回收C3+时拒绝C2，且操作的改变最优选使用程控切换阀和控制切换阀的操作以在需要回收C2+时流体绕过C3+回收交换器且在需要回收C3+时流体绕过C2+回收交换器的关联的控制管路来自动操作。
在如图1中示出的一种例示性构造中，NGL回收成套设备具有流体连接到第二塔(蒸馏塔)61的第一塔(吸收器)58。该成套设备最初设计用于用含有18摩尔% N2、64摩尔% C1、11摩尔% C2、5摩尔% C3、2摩尔% C4和余量的C5 +烃的高氮含量的天然气进料回收C3+且在约100℉的温度和约930psig的压力下供应。本文结合数字使用的术语“约”是指包括数字+/-10。例如，所考虑的温度为“约100℉”的情况下包括90-110℉的温度范围。
下文描述在图1中的C3+回收或C2拒绝操作模式。在此，进料气体进气阀51构造成将进料气体1排他地引导到C3+回收交换器52或C2+回收交换器57。在C3+回收期间，该阀门对交换器52开放且对交换器57和65关闭。进料气流2通过交换器52由残余气流5、分离器液流10和脱甲烷塔塔底物流12冷冻到约-35℉。两相流7闪蒸到分离器53，形成蒸气流14和液流15。液流15经阀门54下降到约400psig的压力并冷冻到约-60℉的温度。该冷冻的物流作为物流10送到交换器52且在闪蒸到脱甲烷塔58的底部之前加热到约20℉，形成物流11。蒸气流14在膨胀机55中膨胀到约370psig且冷冻到约-100℉，形成物流16并进入该吸收器的下段，距塔底至少两个塔板。由该膨胀机生成的动力用于驱动再压缩机56。
在C3+回收操作期间，脱甲烷塔58用来自第二蒸馏塔的塔顶液体的C2富化液流9回流。脱甲烷塔58生成处于约-100℉和约355psig下的塔顶蒸气流19和处于约-20℉下的塔底液流20。该塔顶蒸气与回流罐蒸气流23组合，形成处于约-95℉下的物流5。该组合的物流由进料气流加热到约40℉，形成物流6，物流6由再压缩机56压缩到约440psig，形成物流30A。该残余气体由残余气体压缩机77进一步压缩到约1145psig，形成物流31A，物流31A在交换器78中由冷却水冷却，形成物流32。该残余气体作为物流33在约100℉的温度和约1150psig的压力下直接送到可售气体管线。
脱甲烷塔塔底物流20通过泵60泵压到约375psig，形成物流34，并且在交换器52中加热。将两相流13导引到脱乙烷塔61的中段。该脱乙烷塔生成塔顶蒸气22，塔顶蒸气22在交换器65中通过丙烷制冷而冷却到约-35℉。该两相流随后作为物流25导引通过阀门28且在回流罐66中分离，生成蒸气流23和液流26。将该蒸气流导引以与吸收器塔顶物流19组合且该液流通过泵67泵压到约490psig且随后分成两部分。将约70%作为物流21用作该脱乙烷塔的回流，且剩余部分即物流8用作该脱甲烷塔的回流物流。在脱乙烷塔中的液体通过再沸器62和侧再沸器63汽提，生成具有所要的乙烷-丙烷规格的C3+塔底产物流24。C3操作的典型总体平衡显示在下表中。
表1     C3+回收平衡
该C3+回收成套设备可改造成允许回收C2+且所需的改变用虚线示于图1中。在此，在C2+回收操作期间，将该脱乙烷塔变为脱甲烷塔操作，生成C2+塔底液体。增加专用C2+回收交换器57，其将进料气体回流物流和残余气体回流物流提供到该吸收器，并且绕过交换器52。下文更详细地描述C2+回收操作。
进料气体使用阀门51分成两部分，占该进料气体的约70%的物流3导引到交换器57且剩余部分即物流4导引到丙烷冷冻器65。物流3在回收交换器57中冷冻到约-170℉，形成物流18，物流18经JT阀门69降低压力，并且其作为第二回流导引到该脱甲烷塔。顶部回流(第一塔板回流)通过在约10%-20%的该残余气体冷冻并在交换器57中过冷并且经JT阀门68降低压力之后使该残余物(经物流29)再循环而提供，形成回流物流17。物流4通过丙烷制冷冷却到约-15℉，形成物流35，其经阀门28导引并在交换器73中通过与吸收器塔底物流34热交换而进一步冷却，因此形成物流36。因此，特别优选的成套设备和方法将包括第一C2+交换器(57)和第二C2+交换器(73)。如此冷却的进料气流部分36随后经阀门75导引到分离器53。操作阀门71和阀门72以使得物流34绕过交换器52，在导引到第二塔61之前在交换器73中加热到约-36℉。塔61充当脱甲烷塔，生成塔顶蒸气22和C2+产物24。操作阀门64以将物流22作为物流79再次导引到吸收器塔58的底部。应该注意到，在C2回收期间，物流79充当汽提气体以在吸收器底部除去C1和较轻的组分，其引起生成具有极低C1含量的C2+产物，在该C2+产物中C1含量低至0.0001体积分数。在C2+回收操作期间，以与C3+回收操作类似的方式，将来自分离器53的液流15直接导引到吸收器底部且蒸气流14在膨胀机55中膨胀到约370psig和约-100℉且它们闪蒸到吸收器的下段。
吸收器塔58生成处于约-160℉和约365psig下的塔顶物流19和处于约-60℉下的塔底液流20。该塔顶蒸气作为物流30经阀门59再次导引到C2+回收交换器57，且加热到约65℉，形成物流31，物流31经阀门70导引以便由再压缩机56和残余气体压缩机77压缩。高压残余气体在冷却器78中冷却且约10%-20%作为回流再循环回到吸收器，且余量送到可售气体管线。该操作的总体平衡示于下表中。
表2  C2+回收平衡
因此，应该认识到第一塔(吸收器)塔顶蒸气冷却残余气体并且冷却作为第二回流的进料气体的一部分，残余气体提供塔顶回流(超贫乏)，产生98%的高C2回收率。此外，操作也可通过切换来自第二塔的塔顶的回流而切换到C3+回收(C2拒绝)。在一个优选的方面，在乙烷回收与丙烷回收之间的切换可通过安置成如在图1中所示导引的阀门来操作。这些阀门可构造为多口阀，诸如三通阀，或者其中两个或三个单独的阀门专用于这些操作。阀门切换可程序化且可自动地操作以确保在操作之间的平稳过渡。另外，虽然通常优选该切换以排他方式进行(即，导引到一个目的地或另一目的地)，但在本文中也考虑非排他性切换。所考虑的构造和方法在低能耗下产生98%的高C2回收率，如通过在图2中的C2+回收交换器57的热复合曲线中所证明的密切接近所例示。
关于合适的进料气流，考虑各种进料气流均适合，且特别合适的进料气流可包括不同分子量的各种烃。关于所考虑烃的分子量，通常优选该进料气流主要包含C1-C6烃，且含有高百分数的氮气。然而，合适的进料气流可另外包含酸性气体及其他气态组分(例如，氢气)。因此，特别优选的进料气流为天然气和天然气加工液态产物。
最优选所考虑的成套设备和方法将采用具有吸收器和蒸馏塔的双塔式NGL回收成套设备构造，其中该吸收器构造成接收交替回流物流，允许C3+回收通过来自该蒸馏塔的塔顶液体的回流物流操作且C2+回收用来自残余气体和来自进料气体的至少一部分的回流物流两者操作。这类成套设备允许至少90%的C2回收率和至少99%的C3+回收率，其中C2回收率具有从2%到98%的灵活性，同时维持99%或更高的C3+回收率。从另一观点来考虑，应该认识到所考虑的方法和构造包括第一塔和第二塔，其利用高压残余气体再循环以提供作为第一回流的超贫乏回流和作为用于C2+回收的第二回流的冷冻的进料气体的至少一部分，以及用于C3+回收的包含来自蒸馏塔的塔顶液体的交替回流，同时将冷冻的进料气体的至少一部分膨胀至吸收器以便于所有操作。
所考虑的构造在通过增加C2+回收交换器改造现有C3+回收成套设备以便回收C2+方面特别有利，其比针对C2+回收和C3+回收两者设计的新型成套设备更经济。所述构造还使用专用于回收操作的切换阀简化了成套设备操作。因此，应该特别地认识到，在本文提供的构造和方法中，第一塔的冷却需求至少部分地由中间产物流、残余气体再循环、丙烷制冷和涡轮膨胀提供，并且C2回收率水平可通过将残余物再循环流速从0%变到20%而改变。关于C2回收，预期所述构造提供至少90%、更通常至少94%且最通常至少96%的C2回收率，同时预期C3+回收率将为至少95%、更通常至少98%且最通常至少99%。其他相关的构造、预期和方法描述在我们的美国申请US2010/0206003和公开号为WO 2005/045338和WO 2007/014069的国际专利申请中，其全部通过引用结合到本文中来。
因此，已经公开了改进天然气加工液态产物回收的具体实施方案和应用。然而，本领域的技术人员将显而易见在不脱离本文的发明构思的情况可能有在已描述内容之外的许多改进。因此，除了在本发明的精神内之外，本发明的主题不受约束。另外，在解释本说明书和所考虑权利要求的过程中，所有术语均应按照上下文以尽可能最广泛的方式加以解释。具体地说，术语“包含”应解释为以非排他性的方式提及元件、部件或步骤，表明可存在或利用所提及的元件、部件或步骤或者它们与其他没有明确提及的元件、部件或步骤组合。此外，在通过引用结合到本文中的参考文献中的术语的定义或使用与本文提供的术语的定义不一致或相反的情况下，适用本文提供的术语的定义，而不适用参考文献中的术语的定义。

Claims (12)

1.改造天然气加工液态产物成套设备以回收C2+烃的方法，其中所述天然气加工液态产物成套设备具有吸收器、下游蒸馏塔和构造成冷却进料气体并冷却来自所述蒸馏塔的塔顶产物以由此形成用于所述吸收器的回流物流的C3+回收交换器，且其中将所述吸收器的塔底产物进料到所述下游蒸馏塔，所述方法包括：
对于所述C3+回收交换器安装包括第一专用C2+回收交换器和第二专用C2+回收交换器的旁通管路；
其中所述第一C2+回收交换器使用来自吸收器塔顶产物的制冷容量以由一部分压缩的残余气体生成超贫乏回流物流并由所述进料气体的一部分生成回流物流；
其中所述第二C2+回收交换器使用来自所述吸收器塔底产物的制冷容量以由所述进料气体的另一部分生成冷却的进料气体；和
安装将来自所述蒸馏塔的所述塔顶产物作为汽提蒸气导引到所述吸收器的旁路。
2.权利要求1的方法，其还包括安装将所述冷却的进料气体的液体部分提供到所述吸收器的管路的步骤。
3.权利要求1的方法，其还包括安装控制切换阀的操作以在需要回收C2+时流体绕过所述C3+回收交换器的控制管路的步骤。
4.权利要求1的方法，其还包括使用所述蒸馏塔的塔顶冷凝器以生成所述冷却的进料气体的步骤。
5.权利要求1的方法，其中在将所述冷却的进料气体的蒸气部分进料到所述吸收器之前使所述蒸气部分膨胀到吸收器的压力。
6.改造天然气加工液态产物成套设备以回收C2+烃的方法，其中所述天然气加工液态产物成套设备具有吸收器、下游蒸馏塔和构造成冷却进料气体并冷却来自所述蒸馏塔的塔顶产物以由此形成用于所述吸收器的回流物流的C3+回收交换器，且其中将所述吸收器的塔底产物进料到所述下游蒸馏塔，所述方法包括：
安装第一专用C2+回收交换器和第二专用C2+回收交换器、管道和多个切换阀，使得：
(a) 所述进料气体流排他地导引到所述C3+回收交换器或所述第一C2+回收交换器和所述第二C2+回收交换器；
其中所述C3+回收交换器构造成由所述进料气体生成冷却的进料气体，其中所述第一C2+回收交换器构造成由所述进料气体的第一部分生成进料气体回流物流，且其中所述第二C2+回收交换器构造成由所述进料气体的第二部分生成冷却的进料气体；
(b) 所述吸收器的塔底产物流排他地导引到所述C3+回收交换器或所述第二C2+回收交换器以将制冷容量提供到所述C3+回收交换器或所述第二C2+回收交换器；
(c) 所述吸收器的塔顶产物流排他地导引到所述第一C2+回收交换器以提供制冷容量以由一部分压缩的残余气体产生用于所述吸收器的超贫乏回流物流；和
(d) 所述蒸馏塔的塔顶产物流作为汽提蒸气排他地导引到所述吸收器或作为用于所述吸收器的回流物流排他地导引到所述吸收器和作为蒸馏塔回流排他地导引到所述蒸馏塔。
7.权利要求6的方法，其中所述切换阀中的至少一个为三通阀。
8.权利要求6的方法，其还包括安装控制所述切换阀的操作以在需要回收C2+时绕过所述C3+回收交换器的控制管路的步骤。
9.权利要求6的方法，其还包括流体连接所述蒸馏塔的塔顶冷凝器与所述第二C2+回收交换器以由所述进料气体的第二部分生成冷却的进料气体的步骤。
10.用于改造天然气加工液态产物成套设备以回收C2+烃的套装，其中所述天然气加工液态产物成套设备具有吸收器、下游蒸馏塔和构造成冷却进料气体并冷却来自所述蒸馏塔的塔顶产物以由此形成用于所述吸收器的回流物流的C3+回收交换器，且其中将所述吸收器的塔底产物进料到所述下游蒸馏塔，所述套装包括：
第一专用C2+回收交换器和第二专用C2+回收交换器、管道和多个切换阀，其中：
(a) 第一组阀门和管道构造成允许将进料气体排他地导引到所述C3+回收交换器或所述第一C2+回收交换器和所述第二C2+回收交换器；
其中所述C3+回收交换器构造成由所述进料气体生成冷却的进料气体，其中所述第一C2+回收交换器构造成由所述进料气体的第一部分生成进料气体回流物流，且其中所述第二C2+回收交换器构造成由所述进料气体的第二部分生成冷却的进料气体；
(b) 第二组阀门和管道构造成允许将所述吸收器的塔底产物排他地导引到所述C3+回收交换器或所述第二C2+回收交换器以将制冷容量提供到所述C3+回收交换器或所述第二C2+回收交换器；
(c) 第三组阀门和管道构造成允许将所述吸收器的塔顶产物排他地导引到所述第一C2+回收交换器，且其中所述第一C2+回收交换器构造成将来自所述吸收器塔顶产物的制冷容量提供到一部分压缩的残余气体以产生用于所述吸收器的超贫乏回流物流；和
(d) 第四组阀门和管道构造成允许将来自所述蒸馏塔的塔顶产物作为汽提蒸气排他地导引到所述吸收器或作为用于所述吸收器的回流物流排他地导引到所述吸收器并作为蒸馏塔回流排他地导引到所述蒸馏塔。
11.权利要求10的套装，其中所述切换阀中的至少一个为三通阀。
12.权利要求10的套装，其还包括控制管路，所述控制管路构造成控制所述切换阀的操作以在需要回收C2+时流体隔开所述C3+回收交换器与所述进料气体。
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Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10451344B2 (en) 2010-12-23 2019-10-22 Fluor Technologies Corporation Ethane recovery and ethane rejection methods and configurations
FR2992972B1 (fr) * 2012-07-05 2014-08-15 Technip France Procede de production d'un gaz naturel traite, d'une coupe riche en hydrocarbures en c3+, et eventuellement d'un courant riche en ethane, et installation associee
WO2014047464A1 (en) * 2012-09-20 2014-03-27 Fluor Technologies Corporation Configurations and methods for ngl recovery for high nitrogen content feed gases
WO2014151908A1 (en) * 2013-03-14 2014-09-25 Fluor Technologies Corporation Flexible ngl recovery methods and configurations
CA2855383C (en) * 2014-06-27 2015-06-23 Rtj Technologies Inc. Method and arrangement for producing liquefied methane gas (lmg) from various gas sources
EP3201549B1 (en) 2014-09-30 2019-11-27 Dow Global Technologies LLC Process for increasing ethylene and propylene yield from a propylene plant
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
US10323610B2 (en) * 2016-01-11 2019-06-18 Ford Global Technologies, Llc Noise attenuation device for an intake system of an internal combustion engine
US10330382B2 (en) 2016-05-18 2019-06-25 Fluor Technologies Corporation Systems and methods for LNG production with propane and ethane recovery
US11725879B2 (en) 2016-09-09 2023-08-15 Fluor Technologies Corporation Methods and configuration for retrofitting NGL plant for high ethane recovery
CN108424781A (zh) * 2017-02-15 2018-08-21 中国石油天然气股份有限公司 蒸馏装置液化气收集方法及系统
US11543180B2 (en) * 2017-06-01 2023-01-03 Uop Llc Hydrocarbon gas processing
MX2020003412A (es) 2017-10-20 2020-09-18 Fluor Tech Corp Implementacion de fase de plantas de recuperacion de liquido de gas natural.

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4509967A (en) * 1984-01-03 1985-04-09 Marathon Oil Company Process for devolatilizing natural gas liquids
US6354105B1 (en) * 1999-12-03 2002-03-12 Ipsi L.L.C. Split feed compression process for high recovery of ethane and heavier components
CN101815915A (zh) * 2007-08-14 2010-08-25 氟石科技公司 用于改进的天然气液回收的配置和方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4278457A (en) 1977-07-14 1981-07-14 Ortloff Corporation Hydrocarbon gas processing
US4854955A (en) 1988-05-17 1989-08-08 Elcor Corporation Hydrocarbon gas processing
US5890378A (en) 1997-04-21 1999-04-06 Elcor Corporation Hydrocarbon gas processing
US5890377A (en) 1997-11-04 1999-04-06 Abb Randall Corporation Hydrocarbon gas separation process
US5953935A (en) 1997-11-04 1999-09-21 Mcdermott Engineers & Constructors (Canada) Ltd. Ethane recovery process
US6116050A (en) * 1998-12-04 2000-09-12 Ipsi Llc Propane recovery methods
US6244070B1 (en) 1999-12-03 2001-06-12 Ipsi, L.L.C. Lean reflux process for high recovery of ethane and heavier components
US6823692B1 (en) * 2002-02-11 2004-11-30 Abb Lummus Global Inc. Carbon dioxide reduction scheme for NGL processes
US7051553B2 (en) * 2002-05-20 2006-05-30 Floor Technologies Corporation Twin reflux process and configurations for improved natural gas liquids recovery
US8209996B2 (en) * 2003-10-30 2012-07-03 Fluor Technologies Corporation Flexible NGL process and methods
US9410737B2 (en) 2005-07-25 2016-08-09 Fluor Corporation NGL recovery methods and configurations
US8528361B2 (en) * 2010-10-07 2013-09-10 Technip USA Method for enhanced recovery of ethane, olefins, and heavier hydrocarbons from low pressure gas

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4509967A (en) * 1984-01-03 1985-04-09 Marathon Oil Company Process for devolatilizing natural gas liquids
US6354105B1 (en) * 1999-12-03 2002-03-12 Ipsi L.L.C. Split feed compression process for high recovery of ethane and heavier components
CN101815915A (zh) * 2007-08-14 2010-08-25 氟石科技公司 用于改进的天然气液回收的配置和方法

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