CN1277095C - 液化天然气生产过程中的集成高压天然气液体回收方法 - Google Patents

液化天然气生产过程中的集成高压天然气液体回收方法 Download PDF

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CN1277095C
CN1277095C CNB2004100368664A CN200410036866A CN1277095C CN 1277095 C CN1277095 C CN 1277095C CN B2004100368664 A CNB2004100368664 A CN B2004100368664A CN 200410036866 A CN200410036866 A CN 200410036866A CN 1277095 C CN1277095 C CN 1277095C
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methane
cooling
rich
logistics
stream
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CN1539930A (zh
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M·J·罗伯特斯
H·C·罗勒斯
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Abstract

从天然气中回收比甲烷重的组分的方法，其中所述方法包括：(a)将天然气原料冷却以提供冷却的天然气原料并将冷却的天然气原料在第一位置导入到吸收塔中；(b)从吸收塔中取出比甲烷重的组分被贫化的第一塔顶蒸汽物流，和富含比甲烷重的组分的塔底物流；(c)将富含甲烷的回流物流在高于第一位置的第二位置导入吸收塔中；(d)将塔底物流分离成富含甲烷的物流和一股或多股富含比乙烷重的组分的物流；和(e)将含有比乙烷重的组分的吸收液在第一位置与第二位置之间的位置导入到吸收塔中。

Description

液化天然气生产过程中的集成高压天然气液体回收方法
背景技术
粗天然气主要包括甲烷，同时也包含众多次要成分，其可以包括水、硫化氢、二氧化碳、汞、氮气和通常含2-6个碳原子的轻质烃。这些成分中的一些，比如水、硫化氢、二氧化碳和汞是对下游步骤，比如天然气加工或液化天然气(LNG)生产有害的杂质，这些杂质必须在这些加工步骤的上游去除。比甲烷重的烃通常被冷凝和以天然气液体(NGL)的形式回收并分馏得到有价值的烃产品。
NGL回收使用冷却、部分冷凝和分馏步骤，它们需要大量的致冷。这种致冷可以由加压天然气原料的功膨胀和所得冷凝烃的汽化来提供。或者或是另外，所述致冷可以由使用致冷剂，如丙烷的外部闭环致冷作用来提供。人们希望能在不明显降低天然气压力的情况下从加压天然气回收NGL。这就使得天然气产品(比如管输天然气或LNG)在提供时可处于进料压力或者略低于进料压力的条件下，从而不需要原料和/或产品的再压缩。
为了在接近于进料压力下回收NGL和天然气产品同时又能将致冷能量消耗降到最小，需要改进的NGL回收方法。以下描述的本发明提供一种改进的贫油吸收型NGL回收方法，这一方法可以在明显高于甲烷临界压力的压力下操作，其中在方法中不需要降低天然气的进料压力。
发明内容
本发明的实施方案包括从天然气中回收比甲烷重的组分的方法，其中所述方法包括：
(a)将天然气原料冷却以提供冷却的天然气原料并将冷却的天然气原料在第一位置导入到吸收塔中；
(b)从吸收塔中取出比甲烷重的组分被贫化的第一塔顶蒸汽物流，和富含比甲烷重的组分的塔底物流；
(c)将富含甲烷的回流物流在高于第一位置的第二位置导入吸收塔中；
(d)将塔底物流分离成富含甲烷的物流和一股或多股富含比乙烷重的组分的物流；和
(e)将含有比乙烷重的组分的吸收液在第一位置与第二位置之间的位置导入到吸收塔中。
该方法还可以包括将(d)中一股或多股富含比乙烷重的组分的物流的全部或者其中任意的一部分与(c)中富含甲烷的回流物流混合。或者，该方法还可以包括将(d)中一股或多股富含比乙烷重的组分的物流的全部或者其中任意的一部分作为产物流取出。天然气原料可以处于600psia以上的压力下。
吸收液可以包括从(d)中任意的一股或多股富含比乙烷重的组分的物流所得到的组分。所述吸收液可以包括50摩尔％以上含有5个或5个以上碳原子的烃。或者，所述吸收液可以包括50摩尔％以上含有4个或4个以上碳原子的烃。在另一个备选方案中，所述吸收液可以包括50摩尔％以上含有3个或3个以上碳原子的烃。
吸收液可以在导入到吸收塔中之前通过使用汽化再循环致冷剂的间接换热冷却，这种汽化再循环致冷剂可以是丙烷。
该方法还可以包括将第一塔顶蒸汽物流冷却或者部分冷凝以形成两相物流，将该两相物流分离以得到第二塔顶蒸汽物流和(c)中富含甲烷的回流物流。第二塔顶蒸汽物流可以作为比甲烷重的组分被贫化的产物流回收。(d)中一股或多股富含甲烷的物流的全部或者其中任意的一部分可以在分离两相物流之前与第一塔顶蒸汽物流混合。
用于将第一塔顶蒸汽物流冷却或者部分冷凝的致冷作用可以由使用汽化致冷剂的间接换热提供，这种汽化致冷剂可以是多组分致冷剂。
该方法还可以包括将第二塔顶蒸汽物流冷却、冷凝和过冷以提供液化的天然气产品。将第二塔顶蒸汽物流冷却、冷凝和过冷所需的全部致冷或者其中的一部分可以由使用汽化致冷剂的间接换热提供，这种汽化致冷剂可以是多组分致冷剂。
将第二塔顶蒸汽物流冷却、冷凝和过冷所需的全部致冷或者其中的一部分可以由使用冷致冷剂的间接换热提供，这种冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。
天然气原料冷却的全部或者其中的一部分可以由使用一股或多股汽化致冷剂物流的间接换热提供，这种汽化致冷剂可以是丙烷。
该方法还可以包括由使用来自于吸收塔的液体塔底物流的间接换热来提供天然气原料冷却的一部分，从而得到汽化的塔底物流并将其导入到吸收塔中以提供蒸出蒸汽。
该方法还包括将(d)中富含甲烷的物流进行冷却、冷凝和过冷以提供液化的富含甲烷的产品。将富含甲烷的物流进行冷却、冷凝和过冷所需致冷的全部或其中的一部分可以由使用汽化致冷剂的间接换热提供。或者，将富含甲烷的物流进行冷却、冷凝和过冷所需致冷的全部或其中的一部分可以由使用冷致冷剂的间接换热提供，这种冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。液化的富含甲烷的产品可以与液化的天然气产品结合。
本发明的实施方案也包括从天然气中回收比甲烷重的组分的系统，其中所述系统包括：
(a)用于将天然气分离成富含甲烷的物流和富含比甲烷重的组分的物流的吸收塔；
(b)将天然气冷却以提供冷却的天然气原料的装置和将冷却的天然气原料在吸收塔的第一位置导入到吸收塔中的装置；
(b)从吸收塔中取出比甲烷重的组分被贫化的第一塔顶蒸汽物流和富含比甲烷重的组分的塔底物流的装置；
(c)将富含甲烷的回流物流在高于第一位置的第二位置导入吸收塔中的装置；
(d)将塔底物流分离成富含甲烷的物流和一股或多股富含比乙烷重的组分的物流的分离装置；和
(e)将含有比乙烷重的组分的吸收液在第一位置与第二位置之间的位置导入到吸收塔中的装置。
该系统还包括将第一塔顶蒸汽物流冷却和部分冷凝以形成两相物流的装置和将该两相物流分离以得到第二塔顶蒸汽物流和富含甲烷的回流物流的装置。该系统还可以包括主换热器，在其中具有用于将第一塔顶蒸汽物流冷却和部分冷凝的流动通道(所述冷却和部分冷凝是由使用汽化的多组分致冷剂的间接换热完成的)，具有用于冷却压缩的多组分致冷剂的流动通道，用于降低多组分致冷剂的压力以得到汽化的多组分致冷剂的降压装置，和用于在主换热器中分配所述汽化的多组分致冷剂的装置。
该系统还可以在主换热器中包括另外用于将第二塔顶蒸汽物流冷却和至少部分冷凝以获得液化的天然气产品的流动通道。另外，该系统还可以包括产品换热器，其中，液化的天然气产品被使用冷致冷剂的间接换热进一步冷却，所述冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。
发明详述
根据本发明的实施方案，天然气液体(NGL)是通过吸收方法从加压天然气中回收的，其中冷却的天然气原料流被导入到吸收塔中，通过吸收塔塔顶物流的部分冷凝以及将冷凝物作为回流液返回到塔中而得到富含甲烷的回流物流，和将吸收液在中间位置导入到吸收塔中。这种吸收液可以通过以下方式获得：即将来自于吸收塔的液态塔底物流进行分馏以获得一股或多股含有比乙烷重的烃的液体物流并将这些物流中至少一股物流的一部分或全部返回以提供吸收液。该吸收液被导入到吸收塔中，其导入位置介于导入原料与导入富含甲烷的回流物流的位置之间。该NGL回收方法可以与天然气液化方法集成在一起以便把一部分为最终气体液化所提供的致冷用于冷凝吸收塔塔顶物。分离NGL组分的分馏方法优选用于制备吸收液。
在唯一的附图中阐明了本发明的一个示例性实施方案，其中用于NGL回收与LNG生产的致冷作用由高水平丙烷致冷、使用含甲烷与乙烷的混合致冷剂的中等水平致冷以及低水平膨胀致冷的组合提供。丙烷致冷用于将加压的预处理天然气原料冷却到NGL吸收塔的操作温度和用于将混合致冷剂冷凝。混合致冷剂用于将来自于NGL吸收塔的富含甲烷的塔顶蒸汽冷却和冷凝以及用于向吸收塔顶部提供富含甲烷的回流物流。气体膨胀致冷用于将冷凝的LNG过冷到充分的程度以将LNG减压到贮存压力(通常为低于约20psia)时的闪蒸汽化损失降到最低。
可以使用任何其他类型的致冷系统或系统组合来为NGL回收与LNG生产提供致冷作用。例如，这种致冷可以由甲烷、乙烷或乙烯和丙烷的级联致冷系统、使用混合致冷剂的单一致冷系统、丙烷预冷的混合致冷剂致冷系统、或双重的混合致冷剂致冷系统来提供。各种不同类型的气体膨胀致冷循环可以引入到任何这些致冷系统中。天然气和/或致冷剂膨胀剂；处理气体或液体的方法物流，也可以在适当的时候引入到所述致冷系统中。本发明的基本实施方案并不依赖于NGL回收与LNG生产中使用的致冷类型。
在这一示例性的实施方案中，管线1中已经经过预处理除去了酸性气体组分硫化氢和二氧化碳的加压天然气原料在换热器3中通过用经由管线5提供的汽化丙烷致冷剂换热而冷却。管线7中的预冷原料气，通常为600-900psia和60-80，进一步在处理系统9中被处理除去水和汞。此时的原料气主要包含甲烷与较低浓度的一种或多种处于C2-C5范围内的重烃。管线11中经过预冷和预处理的原料气被分成两部分，分别经由管线13和15，管线13中的那一部分气体成功地在换热器17中被经由管线19提供的汽化丙烷致冷剂和在换热器21中被经由管线23提供的汽化丙烷致冷剂冷却。管线15中的另一部分气体在换热器25中被经由管线27提供的汽化方法物流(以下进行描述)冷却。管线29中的冷却原料与来自于换热器21的冷却原料结合，并且该结合后的原料流在换热器31中被经由管线33提供的汽化丙烷进一步冷却。
管线35中的结合原料流，通常为-20到-40，在吸收塔37的中间点或第一位置上通过吸收塔37。该塔将原料分离成富含重烃的塔底液与富含甲烷的第一塔顶蒸汽。一部分塔底液经由管线27取出，并在先前所述的换热器25中汽化，所得蒸汽流经管线39以提供吸收塔37中的蒸出蒸汽。另一部分塔底液，通常描述为天然气液体(NGL)经由管线41流到NGL分馏器43中。在这里，NGL被使用公知的分馏方法，包括脱乙烷塔、脱丙烷塔和/或脱丁烷塔分馏得到两种或多种烃馏分。在该实施例中，管线41中的塔底物流被分离成管线45中含有甲烷和乙烷的轻馏分，管线47中主要包含丙烷的馏分，管线49中主要包含C4烃的馏分，和管线51中主要包含C5和重烃的馏分。如果需要的话，也可以生成独立的富含乙烷的馏分。
管线51中的一部分C5和重烃经由管线53取出，通过泵55泵送，在换热器57中由经由管线59的汽化丙烷致冷剂冷却，并通过管线61返回，得到去向吸收塔37中的吸收液，其导入位置高于经由管线35导入原料的第一位置。吸收液用于吸收向上通过吸收塔的原料气中的重烃。其余的C5和重烃经由管线52取出。
在选择性的实施方案中，管线49和47中的那部分C4和/或C3烃可以取出和导入到管线53中以形成稍微轻一些的吸收液。在另一个实施方案中，吸收液可以包括C3和/或C4烃而不含C5 +烃。从NGL分馏器43中回收的任何烃液或液体混合物可以用作吸收塔37中的吸收液。对于吸收液组成的选择将根据希望的最终LNG产品的组成和希望的具体NGL组分的回收率来确定。
在非常大的LNG生产装置中，可能要求多个平行的液化系列设备，各个设备将包括原料预处理和冷却步骤、吸收塔37、主换热器67、LNG过冷却器83、和有关的容器和管线。通用的NGL分馏系统可以用于分馏在多个气体液化系列设备中冷凝的组合NGL物流。在该实施方案中，用于各个吸收塔的吸收液将由该通用的NGL分馏系统提供。
主要包含甲烷与少量乙烷、丙烷以及C5 +烃的塔顶蒸汽，通常为-15到-35，通过管线63从吸收塔中取出，在主换热器67的示意的流动通道65中冷却和部分冷凝，并在分离容器或回流储油罐69中分离成蒸汽与液流。分离后的液流主要包含甲烷与来自于吸收塔37塔项中的大部分的乙烷、丙烷和C5 +烃，经由管线71从回流储油罐69中取出。该液体被泵73泵送并流经管线75以提供去向吸收塔37顶部的富含甲烷的回流液，该回流液在第二位置导入，所述第二位置高于通过管线61导入吸收液的第一位置。
富含甲烷的第二塔顶蒸汽通过管线77从回流储油罐69中取出并在主换热器67的示意的流动通道79中冷却和冷凝形成液化的天然气(LNG)。温度为-150到-180的液体经由管线81流到LNG过冷却换热器83中，在那里，该液体在示意的流动通道85中过冷到-180到-240。过冷液通过阀87内蒸，经由管线89进入到产品储罐91中，并分离成管线93中的最终LNG产品和管线95中的剩余闪蒸气体。
在NGL分馏器43中回收的管线45中的甲烷与乙烷在主换热器67的示意的流动通道97中冷却和冷凝，得到额外的液体产品。该液体产品经由管线99取出，在LNG过冷却器83的示意的流动通道101中过冷，通过阀103闪蒸，经由管线89进入到产品储罐91中以得到额外的LNG产品。
用于上述方法的致冷可以，例如通过循环的液态丙烷致冷剂达到第一或者最温暖的温度范围，通过循环的多组分液态致冷剂达到第二或者中间温度范围，和通过冷的气态致冷剂达到第三或者最冷的温度范围。在一个实施方案中，在管线5、19、23、33和57中处于几个温度水平的液态丙烷致冷剂可以由本领域公知类型的任何循环丙烷致冷系统提供。其他致冷剂，比如丙烯或氟利昂可以替代丙烷用在第一或者是最温暖的温度范围中。
压缩的多组分液态致冷剂可以经由管线105提供给主换热器67，其中，所述致冷剂在示意的流动通道107中过冷，通过阀109闪蒸，并经由管线111导入到分配器113中。多组分致冷剂在主换热器67中汽化以在其中提供致冷作用，并且，汽化后的致冷剂经由管线115取出并返回到致冷剂压缩与冷凝系统中(未示出)。用于LNG过冷却器83的致冷作用可以由冷的致冷剂，如氮或含氮混合物经由管线117提供，它在示意的流动通道119中变热以在过冷却器83中提供致冷作用。变热的致冷剂经由管线121返回到在管线117中提供冷致冷剂的压缩与气体膨胀系统(未示出)中。或者，用于NGL回收与LNG生产的致冷作用可以由甲烷、乙烷或乙烯与丙烷的级联致冷系统、使用混合致冷剂的单一致冷系统、丙烷预冷的混合致冷剂致冷系统、或双重的混合致冷剂致冷系统来提供。各种不同类型的气体膨胀致冷循环可以引入到任何这些致冷系统中。
该方法是改进的贫油(C4-C6 +)吸收型NGL回收方法，它利用通用的致冷系统来生产LNG和回收NGL。从原料气中分离NGL所需的中等水平的致冷，如乙烷、乙烯或多组分致冷剂的致冷仅仅占生产LNG所需全部致冷作用的一小部分。
用于NGL吸收塔的富甲烷回流液在冷却富含甲烷的吸收塔塔顶蒸汽的过程中产生，上述蒸汽中还包含有在将C4-C6 +吸收液导入所述塔中时闪蒸的大部分C4-C6 +组分。将这些重烃在吸收塔的顶部导入增加了上部塔区蒸汽与液体混合物的临界压力，并使得所述塔在明显高的压力，比如高于甲烷的临界压力(673psia)下操作，从而不需要降低天然气原料的压力。在分馏器43中产生的一部分C4-C6 +吸收液或另一种重烃液体或液体混合物任选可以与管线71或75中的富甲烷回流液混合或者在于主换热器67的流动通道65中冷却之前或之后与来自于吸收塔37的第一塔顶蒸汽流63混合。这将进一步增加吸收塔顶部蒸汽与液体混合物的临界压力并且如果需要的话，使得所述塔在略微高一些的压力下操作。
该方法还利用分离NGL组分所需的分馏方法来生成重烃(C4-C6 +)吸收液，这使得NGL可以在不降低天然气原料流压力的情况下得以回收。
在尽可能高的压力下操作LNG生产设备会提高富甲烷LNG物流的冷凝温度范围并显著降低为液化方法提供致冷作用所需的能量。在C4-C6 +吸收液进料点之上将富甲烷回流液导入到NGL吸收塔区中也会避免出现最终的LNG产品被重烃污染的问题。
当不需要NGL回收时，这种改进的贫油吸收方法也可以用于从天然气原料流中脱除具有高凝固点的重烃。这将防止LNG生产所需的低温下的凝固与堵塞问题。在这种情况下，分馏部分可以，例如只由脱丁烷塔及相关的再沸器与塔顶冷凝器组成，用于生产作为塔底产物的重烃(C5 +)吸收液并从塔顶排出较轻组分。这些较轻组分任选可以作为LNG回收。如果使用C4 +重烃吸收液，则分馏部分可以只包括脱丙烷塔以及相关的再沸器与塔顶冷凝器，用于生产作为塔底产物的重烃(C4 +)吸收液并从塔顶排出较轻组分。
任选，上述改进的贫油吸收方法在操作时可以不液化加工过的天然气。这将使得天然气原料可以进行用于NGL回收的加工并且在接近于原料压力的条件下得到纯化的天然气产品，当天然气产品以管道气的形式运输时这是有利的。
在选择性的实施方案中，原料将在塔的底部导入到吸收塔37中，将不使用再沸器25，并且所述塔将仅用精馏区操作。来自于这一选择性的吸收塔的塔底液体将在作为NGL分馏器43的一部分的再沸的脱甲烷塔中分离。
附图说明
唯一的附图是表明本发明实施方案的示意流程图。
具体实施方式
为了阐明本发明的一个实施方案，对上述方法进行方法模拟。参考附图，对天然气进行预处理除去酸性气体(CO2和H2S)(未示出)，以得到管线1中的预处理后的原料，流量为137,824lb摩尔/小时，组成(以摩尔％计)为：氮气3.9％，甲烷87.0％，乙烷5.5％，丙烷2.0％，丁烷0.9％，戊烷和重烃0.7％，温度为98，压力为890psia。在另外的用于除去水和汞的预处理方法9之前，该原料在使用由管线5提供的高水平丙烷致冷剂的换热器3中被预冷到约80。
管线11中的天然气在换热器17、21和31中通过三种另外水平的丙烷致冷剂进一步冷却到-27，并经由管线35进料到NGL吸收塔37中。管线15中的一部分原料气在吸收塔再沸器25中冷却，得到再沸蒸汽，经由管线39到达吸收塔37的底部。来自于分馏器43的重烃(C5-C6 +)吸收液，流量为5835lb摩尔/小时，包含0.5摩尔％的丁烷，42.6摩尔％的戊烷和56.9摩尔％的C6 +烃，温度为-27，压力为847psia，经由管线61进入到NGL吸收塔37中。该吸收液在天然气进料点与塔顶的中间位置进入到吸收塔37中，其中吸收液吸收管线35原料中的大部分C3和重烃。
富含甲烷的第一塔顶蒸汽经由管线63从NGL吸收塔中取出，流量为131998lb摩尔/小时，包含(摩尔％)4.1％的氮气，90.9％的甲烷，4.4％的乙烷，0.2％的丙烷，0.015％的丁烷，和0.4％的戊烷和较重烃，温度为-21，压力为837psia。该塔顶蒸汽在主换热器67的暖端被冷却和部分冷凝并流到-86和807psia的回流储罐69中。经由管线71以5726lb摩尔/小时的流量将冷凝液取出，其包含(摩尔％)1.4％的氮气，74.5％的甲烷，15.2％的乙烷，1.2％的丙烷，0.2％的丁烷，和7.6％的戊烷和较重烃。该富甲烷的液体通过回流泵73经由管线75，以回流物的形式返回到NGL吸收塔37的顶部，用于吸收大部分在通过管线61将吸收液导入到塔中时闪蒸出来的C5 +烃。主换热器67由通过管线105供料的汽化的甲烷-乙烷混合致冷剂致冷，并且汽化后的致冷剂经由管线115返回到压缩、冷却和冷凝系统中(未示出)。
NGL吸收塔37底部的液体经由管线41取出，流量为17387lb摩尔/小时，包含(摩尔％)24.6％的甲烷，15.0％的乙烷，15.2％的丙烷，7.1％的丁烷，和38.0％的戊烷和重烃，温度为72，压力为844psia。该塔底液流到NGL分馏器43中，所述分馏区包括脱乙烷塔、脱丙烷塔和脱丁烷塔以及相关的再沸器及塔顶冷凝器(未示出)。脱乙烷塔以6896lb摩尔/小时的流量生产包含(摩尔％)62.1％甲烷、37.8％乙烷和0.1％丙烷，温度为-23，压力为450psia的塔顶甲烷-乙烷(C1-C2)蒸汽产品。该甲烷-乙烷蒸汽经由管线45流到主换热器67中，在示意的流动通道97中被冷却和冷凝，并经由管线99以液体的形式排出。
分馏器43中的脱丙烷塔生产管线47中的液态塔顶产物，其中包含99.5摩尔％的丙烷，流量为2588lb摩尔/小时，温度为120，压力为245psia。分馏器43中的脱丁烷塔生产的液态塔顶物经由管线49排出，包含95摩尔％的丁烷，流量为1269lb摩尔/小时，温度为113，压力为78psia。脱丁烷塔也以6634lb摩尔/小时的流量生产C5 +液态塔底产物，其包含0.5摩尔％的丁烷，42.6摩尔％的戊烷，和56.9摩尔％的C6 +烃，温度为98，压力为83psia。一部分这种C5 +液态塔底物以799lb摩尔/小时的流量经由管线52以产品的形式取出，其余部分则经由管线53和泵55以5838lb摩尔/小时的流量排出。该物流在换热器57中通过经由管线59供料的丙烷致冷剂冷却到-27，冷却后的物流如前所述经由管线61流到NGL吸收塔37中，作为NGL吸收塔37的吸收液。
来自于回流储油罐69的第二塔顶蒸汽经由管线77以126272lb摩尔/小时的流量排出，其包含(摩尔％)4.3％的氮气，91.6％的甲烷，3.9％的乙烷，0.1％的丙烷和0.1％的丁烷及重烃，温度为-86，压力为807psia。该蒸汽流到主换热器67中，在那里，在示意的流动通道79中冷却并全部冷凝，形成管线81中温度为-177°F的中间液化天然气(LNG)产品。该中间液体产品在LNG过冷却器83的示意流动通道85中过冷到-237，通过阀87闪蒸为15.2psia，并通过管线89流到最终的产品分离器91中。另外的管线99中的液体(先前所述)在LNG过冷却器83的示意流动通道101中过冷，通过阀103闪蒸，也经由管线89流到最终的产品分离器91中。最终的LNG产品经由管线93排出进行贮存，而闪蒸气体则经由管线95排出，作为燃料使用。LNG过冷却器83的致冷作用由管线117中的冷却氮致冷剂提供，它在示意的流动通道119中变暖，变暖的氮经由管线121取出并返回到压缩与功膨胀系统(未示出)中以便经由管线117提供回用的氮气致冷剂。
这一示例性的方法以NGL产物的形式回收天然气原料中92.5％的丙烷，98.6％的丁烷和99.6％的C6及更重的烃。用于NGL分离方法的致冷作用是为天然气产物液化所提供的致冷作用的一部分。在这一实施例中，原料气中大约有74％的戊烷以NGL产品的形式回收，并且这一量足以降低富甲烷LNG产品中的浓度，以防止烃冻结并堵塞吸收塔37下游的冷设备。如果希望的话，通过增加经由管线61回到NGL吸收塔37中的主要为C5 +的吸收液的流量可以提高丙烷的回收率，但是，这也将需要相应地增加经由管线75回到吸收塔37顶部的富甲烷回流液的流量。经由管线61回到NGL吸收塔37的吸收液与经由管线75回到NGL吸收塔37的富甲烷回流液的流量增加将增加该方法所需中等水平致冷作用的量，在该实施例中这一致冷作用是由通过管线105的甲烷-丙烷混合致冷剂提供的。
如果主要将C4烃用作吸收液或者如果将C4烃加入到该实施例的C5-C6 +吸收液中，则C5烃的回收率将会增加，但是管线49中作为NGL产品的C4烃的回收率将会降低。任选，可以将丙烷用作至少一部分经由管线61提供的吸收液，但是这将会明显降低经由管线47作为最终产品回收的丙烷的回收率。对于吸收液组成的选择可以由较重烃作为NGL产品回收时的价值决定，这一价值是相对于其作为最终LNG产品的一部分时的价值而言的。经由管线61提供的吸收液可以是NGL分馏器43中生产的重烃液或其液体混合物的任意组合。

Claims (31)

1.一种从天然气中回收比甲烷重的组分的方法，其中所述方法包括：
(a)将天然气原料冷却以提供冷却的天然气原料并将冷却的天然气原料在第一位置导入到吸收塔中；
(b)从吸收塔中取出比甲烷重的组分被贫化的第一塔顶蒸汽物流，和富含比甲烷重的组分的塔底物流；
(c)将富含甲烷的回流物流在高于第一位置的第二位置导入吸收塔中；
(d)将塔底物流分离成富含甲烷的物流和一股或多股富含比乙烷重的组分的物流；和
(e)将含有比乙烷重的组分的吸收液在第一位置与第二位置之间的位置导入到吸收塔中。
2.权利要求1的方法，还包括将(d)中一股或多股富含比乙烷重的组分的物流的全部或者其中任意的一部分与(c)中富含甲烷的回流物流混合。
3.权利要求1的方法，还包括将(d)中一股或多股富含比乙烷重的组分的物流的全部或者其中任意的一部分作为产物流取出。
4.权利要求1的方法，其中天然气原料压力为600psia以上。
5.权利要求1的方法，其中吸收液包括从(d)中任意的一股或多股富含比乙烷重的组分的物流所得到的组分。
6.权利要求1的方法，其中吸收液包括50摩尔％以上含有5个或5个以上碳原子的烃。
7.权利要求1的方法，其中吸收液包括50摩尔％以上含有4个或4个以上碳原子的烃。
8.权利要求1的方法，其中吸收液包括50摩尔％以上含有3个或3个以上碳原子的烃。
9.权利要求1的方法，其中吸收液在导入到吸收塔中之前通过使用汽化的再循环致冷剂的间接换热进行冷却。
10.权利要求9的方法，其中所述汽化的再循环致冷剂是丙烷。
11.权利要求1的方法，还包括将第一塔顶蒸汽物流冷却和部分冷凝以形成两相物流，将该两相物流分离以得到第二塔顶蒸汽物流和(c)中富含甲烷的回流物流。
12.权利要求11的方法，其中第二塔顶蒸汽物流作为比甲烷重的组分被贫化的产物流回收。
13.权利要求11的方法，还包括将(d)中一股或多股富含甲烷的物流的全部或者其中任意的一部分在分离两相物流之前与第一塔顶物流混合。
14.权利要求11的方法，其中用于将第一塔顶蒸汽物流冷却或者部分冷凝的致冷作用由使用汽化致冷剂的间接换热提供。
15.权利要求14的方法，其中所述汽化致冷剂是多组分致冷剂。
16.权利要求11的方法，还包括将第二塔顶蒸汽物流冷却、冷凝和过冷以提供液化的天然气产品。
17.权利要求16的方法，其中将第二塔顶蒸汽物流冷却、冷凝和过冷所需的全部致冷或者其中的一部分由使用汽化致冷剂的间接换热提供。
18.权利要求17的方法，其中所述汽化致冷剂是多组分致冷剂。
19.权利要求16的方法，其中将第二塔顶蒸汽物流冷却、冷凝和过冷所需的全部致冷或者其中的一部分由使用冷致冷剂的间接换热提供，这种冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。
20.权利要求1的方法，其中天然气原料冷却的全部或者其中的一部分由使用一股或多股汽化致冷剂物流的间接换热提供。
21.权利要求20的方法，其中所述汽化致冷剂是丙烷。
22.权利要求1的方法，还包括由使用来自于吸收塔的液体塔底物流的间接换热来提供天然气原料冷却的一部分，从而得到汽化的塔底物流并将其导入到吸收塔中以提供蒸出蒸汽。
23.权利要求16的方法，还包括将(d)中富含甲烷的物流进行冷却、冷凝和过冷以提供液化的富含甲烷的产品。
24.权利要求23的方法，其中将富含甲烷的物流进行冷却、冷凝和过冷所需致冷的全部或其中的一部分由使用汽化致冷剂的间接换热提供。
25.权利要求23的方法，其中将富含甲烷的物流进行冷却、冷凝和过冷所需致冷的全部或其中的一部分由使用冷致冷剂的间接换热提供，这种冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。
26.权利要求23的方法，其中液化的富含甲烷的产品与液化的天然气产品结合。
27.一种从天然气中回收比甲烷重的组分的系统，其中所述系统包括：
(a)用于将天然气分离成富含甲烷的物流和富含比甲烷重的组分的物流的吸收塔；
(b)将天然气原料冷却以提供冷却的天然气原料的冷却装置和将冷却的天然气原料在吸收塔的第一位置导入到吸收塔中的装置；
(b)从吸收塔中取出比甲烷重的组分被贫化的第一塔顶蒸汽物流和富含比甲烷重的组分的塔底物流的装置；
(c)将富含甲烷的回流物流在高于第一位置的第二位置导入吸收塔中的装置；
(d)将塔底物流分离成富含甲烷的物流和一股或多股富含比乙烷重的组分的物流的分离装置；和
(e)将含有比乙烷重的组分的吸收液在第一位置与第二位置之间的位置导入到吸收塔中的装置。
28.权利要求27的系统，还包括将第一塔顶蒸汽物流冷却和部分冷凝以形成两相物流的装置和将该两相物流分离以得到第二塔顶蒸汽物流和富含甲烷的回流物流的装置。
29.权利要求28的系统，还包括主换热器，在其中具有用于将第一塔顶蒸汽物流由使用汽化的多组分致冷剂的间接换热冷却和部分冷凝的流动通道，具有用于冷却压缩的多组分致冷剂的流动通道，用于降低多组分致冷剂的压力以得到汽化的多组分致冷剂的降压装置，和用于在主换热器中分配所述汽化的多组分致冷剂的装置。
30.权利要求29的系统，还包括在主换热器中的另外用于将第二塔顶蒸汽物流冷却和至少部分冷凝以获得液化的天然气产品的流动通道。
31.权利要求30的系统，还包括产品换热器，其中，液化的天然气产品被使用冷致冷剂的间接换热进一步冷却，所述冷致冷剂是由压缩的含氮致冷剂的功膨胀提供的。
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