CN102741634A - 烃气体处理 - Google Patents
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Abstract
公开了从烃气流中回收乙烷、乙烯和重烃组分的工艺和设备。所述流被冷却、膨胀至较低压力,并且被供应至第一分馏塔的塔中部进料位置。从所述第一分馏塔的低于所述膨胀流的进料位置抽取蒸馏液体流,加热并且引导进入产生顶部蒸气流和底部液体流的第二分馏塔。冷却所述顶部蒸气流以使它冷凝,其中冷凝流的一部分被引导至第二分馏塔以作为其顶部进料,而剩余部分被引导至第一分馏塔的塔下部进料位置。来自第二分馏塔的底部液体流被冷却并引导至第一分馏塔以作为其顶部进料。
Description
发明背景
本发明涉及一种用于分离含烃气流的工艺,其中包含显著量的比甲烷更易挥发的组分(例如氢气、氮气,等等)的含烃气流被分离成两种馏分:主要包含甲烷和更易挥发的组分的第一馏分,以及包含被回收的所需乙烷/乙烯和重烃组分的第二馏分。
乙烯、乙烷、丙烯、丙烷和/或重烃可从各种气体回收,例如天然气、炼油气和获自其它烃类材料(例如煤炭、原油、石油脑、油页岩、沥青砂和褐煤)的合成气流。除甲烷、乙烷和高分子量烃类如丙烷、丁烷和戊烷之外,含烃气体一般还包含比甲烷更易挥发的组分(例如氢气、氮气,等等)以及还经常包含不饱和烃类(例如乙烯、丙烯,等等)和芳香烃类(例如苯、甲苯,等等)。有时也存在含硫气体和二氧化碳。
本发明大体来说是关于从这些气流回收乙烯、乙烷和重(C2+)烃。近期乙烯需求的变化已为乙烯及衍生产品创造了增加的市场。此外,天然气和其液态天然气(NGL)这两种成分的价格波动已然提升了乙烷和作为液态产物的较重组分的价值。这些市场条件导致了对可以提供乙烯和乙烷的高回收以及全部这些产物的更有效回收的工艺的需要。分离这些物质可用的工艺包括基于气体的冷却和冷冻、油吸收和冷冻油吸收的工艺。此外,由于可使用经济的设备,从被处理的气体同时膨胀和提取热时产生动力,因此低温工艺已变得普遍。取决于气体源的压力、气体的丰富性(乙烷、乙烯和重烃含量)和所需的终产物,可使用这些工艺的每一种工艺或其组合。
低温膨胀(cryogenic expansion)工艺现在通常优选用于液态天然气的回收,因为它提供极大的简单性使起动容易、操作灵活、效率佳、安全和可靠性佳。美国专利:第3,292,380号、第4,061,481号、第4,140,504号、第4,157,904号、第4,171,964号、第4,185,978号、第4,251,249号、第4,278,457号、第4,519,824号、第4,617,039号、第4,687,499号、第4,689,063号、第4,690,702号、第4,854,955号、第4,869,740号、第4,889,545号、第5,275,005号、第5,555,748号、第5,566,554号、第5,568,737号、第5,771,712号、第5,799,507号、第5,881,569号、第5,890,378号、第5,983,664号、第6,182,469号、第6,578,379号、第6,712,880号、第6,915,662号、第7,191,617号、第7,219,513号;再公告的美国专利:第33,408号;和共同待决的申请案:第11/430,412号、第11/839,693号、第11/971,491号、第12/206,230号、第12/689,616号、第12/717,394号、第12/750,862号、第12/772,472号、第12/781,259号、第12/868,993号、第12/869,007号和第12/869,139号描述了相关的工艺(尽管与引用的美国专利和申请中描述的相比本发明的描述在某些情况下基于了不同的处理条件)。
在典型的低温膨胀回收工艺中,在带压下的进料气流通过与该工艺中的其它气流和/或外部冷冻源(例如丙烷压缩冷冻系统)的热交换而冷却。随着所述气体被冷却,可冷凝出液体并以包含某些所需C2+组分的高压液体收集在一个或多个分离器中。取决于所述气体的丰富性和形成的液体量,可将所述高压液体膨胀到较低压力并进行分馏。液体膨胀期间发生的蒸发造成该流的进一步冷却。在某些情况下,较理想的是膨胀前预冷却高压液体,以进一步降低膨胀产生的温度。包含液体与蒸气混合物的膨胀气流在蒸馏(去甲烷塔或去乙烷塔)塔中分馏。在所述塔中蒸馏膨胀冷却的气流,以将作为顶部蒸气的残余甲烷、氢气、氮气和其它挥发性气体与作为底部液体产物的所需C2组分、C3组分和重烃组分分离;或将作为顶部蒸气的残余甲烷、C2组分、氢气、氮气和其它挥发性气体与作为底部液体产物的所需C3组分和重烃组分分离。
如果所述进料气体未被完全冷凝(通常未完全),那么所述部分冷凝中剩余的蒸气可通过功膨胀机器(work expansion machine)或发动机,或膨胀阀,达到较低压力,在此压力下,由于流的进一步冷却而冷凝另外的液体。膨胀后的压力基本上与蒸馏塔操作时的压力相同。膨胀作用所得的蒸气-液体组合相作为进料被供应给所述塔。
在此类分离工艺的理想操作中,从该工艺中离去的残余气体将包含进料气体中的实质上所有的甲烷和更易挥发的组分,而基本上不含重烃组分;并且离开去甲烷塔的底馏分将包含实质上所有的重烃组分,而基本上不含甲烷或更易挥发的组分。然而实际上无法得到这种理想情况,因为惯用的去甲烷塔大多作为汽提塔操作。因此所述工艺的甲烷产物通常包含从所述塔的顶部分馏阶段中离去的蒸气,以及未经历任何精馏步骤的蒸气。由于顶部液体进料包含大量的C2+组分和重烃组分,因而发生相当多的乙烯和乙烷损失,在离开去甲烷塔的顶部分馏阶段的蒸气中产生了对应平衡量的C2+组分。在被处理的气流中存在相对大量的比甲烷更易挥发的组分(例如氢气、氮气,等等)的情况下,由于所述塔中上升的挥发性蒸气从下行液体中汽提C2+组分,而使这一问题加剧。如果所述上升的蒸气可以与能够从蒸气吸收C2+组分的大量液体(回流)发生接触,则可显著减少这些所需C2+组分的损失。
已经开发了许多工艺,使用主要为甲烷的冷液体作为回流流在所述蒸馏塔内的精馏段中接触所述上升蒸气。此类型的典型工艺方案公开于美国专利第4,889,545号、第5,568,737号和第5,881,569号,以及Mowrey,E.Ross,"Efficient,High Recovery of Liquids from NaturalGas Utilizing a High Pressure Absorber",天然气处理者协会(GasProcessors Association)第81年周年大会公报(德克萨斯州Dallas,2002年3月11-13日)。不幸的是,这些工艺需要使用压缩机提供原动力将回流流再循环到去甲烷塔,从而增加了使用这些工艺的设备的资本成本和操作成本。此外,所述冷甲烷回流在蒸馏塔中产生了-112°F[-80°C]和更冷的温度。此类型的许多气流有时包含大量的氮氧化物(NOX),在低于此温度的温度下,其可在处理设施的冷却段中以NOX胶(通常称为“蓝冰”)的形式积聚。“蓝冰”在加温下可变得易爆,并且被认定是处理设施中的许多爆燃和/或爆炸的原因。
业已开发了使用重(一般为C4-C10)烃吸附剂流以对所述蒸馏塔进行回流的其它工艺。此类型工艺的实例为美国专利第4,318,723号、第5,546,764号、第7,273,542号和第7,714,180号。虽然这类工艺通常在暖到足以避免“蓝冰”问题的温度下操作,但是所述吸附剂流一般是从所述蒸馏塔底部流中产生,结果导致进料气体中存在的任何芳香烃将会集中于蒸馏塔内。诸如苯这样的芳香烃在正常处理温度下可冷冻成固体,从而在处理设施内造成频繁的破坏。
根据本发明,已发现在无需任何低于-112°F[-80°C]的温度下即可获得超出88%的乙烷回收率。在处理包含超过10摩尔%的比甲烷更易挥发的组分的进料气体时,本发明特别地有利。
为更好地理解本发明,可参考下列实施例和附图。参见附图:
图1是根据本发明的气体处理设施的流程图;以及
图2是说明本发明应用于气流的其它方式的流程图。
在下面对以上附图的阐述中,提供了表格来概述针对代表性工艺条件所计算的流率。在本文所列的表格中,为方便起见,流率(以摩尔/小时为单位)的数值已取整为最接近的整数。表格中所示的总流速率包括所有非烃类组分,因而通常大于烃类组分的流流率的总和。所示的温度是取整至最接近的度数的近似值。还应注意,出于比较附图所描绘的工艺的目的而进行的所述工艺设计的计算,是以周围环境与工艺之间没有相互热泄漏的假设为基础。市售隔热材料的质量使之成为非常合理的假设,且本领域的技术人员通常会作这种假设。
为方便起见,兼以传统英制单位和国际单位制度(SI)的单位记述工艺参数。表格中给出的摩尔流率可解读为磅摩尔/小时或千克摩尔/小时。以马力(HP)和/或千英热单位/小时(MBTU/Hr)记述的能耗对应于以磅摩尔/小时描述的摩尔流率。以千瓦(kW)记述的能耗对应于以千克摩尔/小时描述的摩尔流率。
发明描述
图1示出根据本发明的工艺的流程图。在图1工艺的模拟中,进气在100°F[38°C]和77psia[531kPa(a)]作为流51进入设施。如果所述进气含有会妨碍产流符合规定的浓度的硫化合物和/或二氧化碳,则通过对进料气体的适当预处理除去所述硫化合物和/或二氧化碳(未示出)。
在处理之前将所述进气通过三个阶段压缩至较高的压力(由外部动力源驱动的压缩机10和15,以及由功膨胀机器14驱动的压缩机13)。排气冷却器11和16被用于冷却阶段之间的气体,并且分离器12和17被用于除去在所述气流冷却时从中冷凝出的任何水或其它液体。离开分离器17的冷却了的压缩气流54在脱水单元18中脱水以防止低温条件下的水合物(冰)形成。固体干燥剂一般被用于此目的。
所述脱水了的气流61在100°F[38°C]和560psia[3,859kPa(a)]进入热交换器20并且通过与冷残余气体(流68a)、28°F[-2°C]的液体产物(流71a)、13°F[-11°C]的去甲烷塔再沸器液体(流70)和丙烷制冷剂的热交换进行冷却。需注意,在所有情况下,交换器20代表许多个体热交换器或单个多程热交换器,或其任意组合。(至于是否在所指示的冷却操作中使用一个以上热交换器,将取决于许多因素,包括但不限于进气流率、热交换器大小、流温度等等)。冷却了的流61a在40°F[4°C]和550psia[3,790kPa(a)]进入分离器21,在此处蒸气(流62)与冷凝的液体(流63)分离开来。分离器液体(流63)通过膨胀阀22被膨胀到分馏塔28的操作压力(大约175psia[1,207kPa(a)]),从而使流63a在供应至分馏塔28的塔下部进料点之前冷却至16°F[-9°C]。
来自分离器21的蒸气(流62)在热交换器23中通过与冷残余气体(流68)、-10°F[-23°C]的去甲烷塔侧再沸器液体(流69)、闪蒸液体(流65a)和丙烷制冷剂的热交换而进一步冷却。冷却了的流62a在-42°F[-41°C]和535psia[3,686kPa(a)]进入分离器24,在此处蒸气(流64)与冷凝的液体(流65)分离开来。分离器液体(流65)通过膨胀阀25被膨胀至略高于塔的操作压力,从而使流65a冷却至-63°F[-53°C],之后它在热交换器23中被加热至-40°F[-40°C]。加热了的流65b随后被供应至分馏塔28的塔中下部进料点。
来自分离器24的蒸气(流64)进入功膨胀机器14,在其中从此部分的高压进料中提取机械能。所述机器14将蒸气实质上等熵膨胀至塔操作压力,其中利用功膨胀将膨胀流64a冷却至温度大约为-105°F[-76°C]。典型的市售膨胀机能够回收理想等熵膨胀中理论上可获得的功的80-85%的等级。回收的功通常用于驱动离心式压缩机(例如项目13),举例来说,其可被用于压缩进气(流52)。部分冷凝了的膨胀流64a此后作为进料被供应至分馏塔28的塔中上部进料点。
塔28中的去甲烷塔是惯用的蒸馏塔,其包含多个垂直间隔盘、一个或多个填料床、或盘和填料的某一组合。去甲烷塔由两段构成:上部吸收(精馏)段,其包含所述盘和/或填料用以提供上升的膨胀流64a的蒸气部分与下落的冷液体间的必要接触,以从上升的蒸气中冷凝和吸收C2组分、C3组分和较重组分;以及下部汽提(去甲烷)段,其包含所述盘和/或填料用以提供下落的液体与上升的蒸气间的必要接触。所述去甲烷段还包括一个或多个再沸器(例如前述的再沸器和侧再沸器),其加热和蒸发所述塔中向下流的液体的一部分以提供所述塔中向上流的汽提蒸气用以汽提具有甲烷和较轻组分的液体产物,即流71。流64a进入去甲烷塔28的中间进料位置,其位于去甲烷塔28的吸收段的下部区域。膨胀流的液体部分掺和从所述吸收段下落的液体,并且合并了的液体继续下行进入去甲烷塔28的汽提段。所述膨胀流的蒸气部分上升通过所述吸收段并与下落的冷液体接触用以冷凝和吸收所述C2组分、C3组分和较重组分。
一部分蒸馏液体(流72)被从分馏塔28的汽提段的中间区域抽取,所述中间区域在汽提段内低于所述吸收段的下部区域中的膨胀流64a的进料位置但高于膨胀液体流63a的进料位置。在该位置抽取所述蒸馏液体提供了主要为C2-C5烃的液体流,其包含极少量所述挥发性组分(例如甲烷、氢气、氮气等等)和极少量的所述芳香烃和重烃组分。这一蒸馏蒸气流72通过泵30被泵压至高压(流72a)并且随后在热交换器31中通过与热的去丙烷塔底部流78的热交换,从-25°F[-32°C]被加热至77°F[25°C]并且被部分蒸发。加热了的流72b随后进入去丙烷塔32(在265psia[1,828kPa(a)]下操作)的塔中部进料点。
塔32中的去丙烷塔是惯用的蒸馏塔,其包含多个垂直间隔盘、一个或多个填料床、或盘和填料的某一组合。去丙烷塔由两段构成:上部吸收(精馏)段,其包含所述盘和/或填料用以提供上升的被加热流72b的蒸气部分与下落的冷液体间的必要接触,以冷凝和吸收C4组分和较重组分;以及下部汽提(去丙烷)段,其包含所述盘和/或填料用以提供下落的液体与上升的蒸气间的必要接触。所述去丙烷段还包括一个或多个再沸器(例如再沸器33),其加热和蒸发所述塔中向下流的液体的一部分以提供所述塔中向上流的汽提蒸气用以汽提具有C3组分和较轻组分的底部液体产物,即流78。流72b进入去丙烷塔32的中间进料位置,其位于去丙烷塔32的吸收段与汽提段之间。被加热流的液体部分掺和从所述吸收段下落的液体,并且合并了的液体继续下行进入去丙烷塔32的汽提段。所述被加热流的蒸气部分上升通过所述吸收段并且与下落的冷液体接触用以冷凝和吸收所述C4组分和较重组分。
来自去丙烷塔32的顶部蒸气(流73)进入回流冷凝器34并且被丙烷制冷剂从59°F[15°C]冷却至-33°F[-36°C]以使其在260psia[1,793kPa(a)]进入回流分离器35之前冷凝。如果存在任何未冷凝的蒸气(流74),通过膨胀阀38将它膨胀至去甲烷塔28的操作压力并且回送至去甲烷塔28的塔下部进料点。然而,在图1的模拟中,所有的顶部蒸气被冷凝并在液体流75中离开回流分离器35。流75通过泵36被泵压至略高于去丙烷塔32的操作压力,并且随后流75a的一部分(流76)作为顶部塔进料(回流)被供应给去丙烷塔32以吸收和冷凝在所述塔的吸收段中上升的所述C4组分和较重组分。剩余部分(流77)包含从蒸馏液体流72中汽提出的C3组分和较轻组分。它通过膨胀阀37被膨胀至去甲烷塔28的操作压力,从而使流37a冷却至-44°F[-42°C],之后它被回送至去甲烷塔28的塔下部进料点,其低于蒸馏液体流72的抽取点。
来自去丙烷塔32的所述底部液体产物(流78)已被汽提出所述C3组分和较轻组分,并且主要为C4-C5的烃。它在230°F[110°C]离开去丙烷塔32的底部并且根据前文所述在热交换器31中被冷却至-20°F[-29°C]。流78a使用丙烷制冷剂在热交换器39中被进一步冷却至-35°F[-37°C](流78b)并且随后在膨胀阀40中被膨胀至去甲烷塔28的操作压力。膨胀流78c随后作为回流被供应给去甲烷塔28,在-35°F[-37°C]进入顶部进料位置。流78c中的C4-C5烃充当吸附剂来捕获去甲烷塔28的吸收段内向上流的蒸气中的C2+组分。
在去甲烷塔28的汽提段中,所述进料流被汽提出其甲烷和较轻组分。所产生的液体产物(流71)在24°F[-4°C]离开塔28的底部并且在泵29中被泵压至较高压力。根据前文所述,被泵压了的流71a随后在热交换器20中被加热至93°F[34°C]。冷残余气流68在-32°F[-35°C]离开去甲烷塔28并且如先前所述随着它提供冷却,逆流地在热交换器23中和在热交换器20中流至输入的进料气体,其中在热交换器23处它被加热至32°F[0°C](流68a),在热交换器20中它被加热至95°F[35°C](流68b)。所述残余气体产物随后在165psia[1,138kPa(a)]流入燃气输配管(fuel gas distribution header)。
下表中概述了图1中示出工艺的流流率和能耗。
表I
(图1)
流流率概述-磅摩尔/小时[千克摩尔/小时]
回收率*
功率
进气压缩 6,072HP [9,982kW]
制冷剂压缩 5,015HP [8,245kW]
总压缩 11,087HP [18,227kW]
*(基于未取整的流率)
其它实施方案
根据本发明,设计所述去甲烷塔的吸收(精馏)段使其包含多个理论分离阶段通常是有利的。然而,本发明的益处可由少至两个理论阶段即可达成。举例来说,可将所述回流液体(流78c)的全部或一部分与膨胀流64a的全部或一部分合并(例如在通向所述去甲烷塔的管路中进行),且若彻底掺和,蒸气和液体将混合在一起并根据整个合并流的各种组分的相对挥发性分离。就本发明的目的来说,所述两股流的这种掺和将被视为构成吸收段。
图2示出本发明的另一种实施方案,其在某些情况下可能是优选的。在图2的实施方案中,来自分离器24的蒸气流64的一部分(流66)通过膨胀阀26被膨胀至中度压力并且随后与冷却了的去丙烷塔底部流78b进行合并以形成合并流79。合并流79在热交换器27中通过冷去甲烷塔顶部流68被冷却(流79a),随后通过膨胀阀40被膨胀至去甲烷塔28的操作压力。膨胀流79b随后作为回流被供应至去甲烷塔28的顶部进料位置。蒸气流64的剩余部分(流67)通过功膨胀机器14被膨胀至所述塔操作压力,并且膨胀流67a被供应至去甲烷塔28的塔中上部进料位置。
进料气体条件、设施大小、可用设备或其它因素可能提示了功膨胀机器14的去除或代之以其它的膨胀装置(例如膨胀阀)是可行的。虽然已在具体的膨胀装置中描述了个别的流膨胀,但是适当时可使用其它的膨胀构件。例如,诸多条件可保证所述回流流(流78b或流79a)的功膨胀。
当所述进气较为匮乏时,图1和图2中的分离器21可能无存在必要。在这些情况下,图1和图2中在热交换器20和23内完成的进料气体冷却可在没有介入分离器的情况下实现。至于是否在多步骤内冷却和分离所述进料气体,将取决于进料气体的丰富性、设施大小、可用的设备等等。取决于进料气体中重烃的量和进料气体的压力,图1和图2中离开交换器20的冷却了的进料流61a和/或离开热交换器23的冷却了的流62a可能不包含任何液体(由于高于其露点,或由于高于其临界凝结压力),从而不需要图1和图2中示出的分离器21和/或分离器24。
在被供应至所述分馏塔的塔中下部进料点之前,所述膨胀了的液体(图1和图2中的流65a)无需进行加热。相反,其全部或部分可被直接供应给所述塔。随后,所述膨胀了的液体的任何剩余部分可在被进料于所述蒸馏塔之前进行加热。
根据本发明,可使用外部冷冻以对来自其它工艺流的进气可用的冷却作用进行补充,特别是在丰富进气的情况下。和用于特定热交换服务的工艺流的选择一样,用于过程热交换的分离器液体和去甲烷塔侧抽液体的使用和分配,以及用于进气冷却的热交换器的具体布置都必须针对每一具体应用进行评估。
根据本发明,可用多种方式实现图2实施方案中蒸气进料的分束。在图2的工艺中,随着可能已经形成的任意液体的冷却和分离之后而发生蒸气的分束。但是,所述高压气体可在所述进气的任意冷却之前或在所述气体冷却之后和任意分离阶段之前被分束。在一些实施方案中,蒸气分束可在分离器中实现。
还应认识到,在图2实施方案中被分束的蒸气进料的每一分流中所见的进料的相对量将取决于若干因素,包括气体压力、进料气体组成、从进料可节约提取的热量,和可用的马力量。对所述塔顶部的更多进料可增加回收率,同时减低从所述膨胀器中回收的功率,从而增加压缩马力需求。增加在所述塔下部的进料降低了马力消耗,但也会降低产物回收率。取决于进入组成或例如所需的回收程度和在进气冷却期间所形成的液体的量等其它因素,塔中部进料的相对位置可有所变化。此外,取决于个别流的相对温度和量,进料流中的两个或更多个流或其部分可进行合并,然后合并了的流被进料于塔中部进料位置。
按照操作所述工艺所需的每单位量的动力消耗指标(utilityconsumption)来说,本发明提供了C2组分、C3组分和重烃组分的改进回收率。操作去甲烷塔工艺所需的动力消耗指标的改进可体现为压缩或再压缩的功率需求降低、外部冷冻的功率需求降低、塔再沸器的能需降低或其组合的形式。
尽管已描述了被视为本发明的优选实施方案的内容,然而本领域的技术人员应认识到可对所述优选实施方案做其它和进一步的修改,例如使本发明适合于多种条件、进料的种类,或其它需求,而不背离由随附权利要求所界定的本发明的精神。
Claims (16)
1.一种用于分离气流的工艺,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在该工艺中:
(a)所述气流在带压下被冷却以提供冷却流;
(b)所述冷却流被膨胀至较低压力,从而进一步被冷却;以及
(c)所述进一步冷却了的流被引导进入第一蒸馏塔并且在所述较低压力下分馏,由此回收所述挥发性相对较低的馏分的所述组分;
其中改进之处在于
(1)所述进一步冷却了的膨胀流被引导至所述第一蒸馏塔的塔中部进料位置;
(2)从所述第一蒸馏塔的低于所述塔中部进料位置的区域抽取蒸馏液体流;
(3)所述蒸馏液体流被加热,并且随后被引导进入第二蒸馏塔并且分馏成为顶部蒸气流和底部液体流;
(4)所述顶部蒸气流被冷却以实质上全部冷凝,从而形成冷凝流;
(5)所述冷凝流被分成第一部分和第二部分,由此所述第一部分被引导至所述第二蒸馏塔的顶部进料位置;
(6)所述第二部分被引导至所述第一蒸馏塔的塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域;
(7)所述底部液体流被冷却,从而供应步骤(3)的至少一部分加热作用;
(8)所述冷却了的底部液体流被引导至所述第一蒸馏塔的顶部进料位置;
(9)进入所述第二蒸馏塔的所述进料流的量和温度有效地将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(10)进入所述第一蒸馏塔的所述进料流的量和温度有效地将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
2.一种用于分离气流的工艺,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在该工艺中:
(a)所述气流在带压下被冷却以提供冷却流;
(b)所述冷却流被膨胀至较低压力,从而进一步被冷却;以及
(c)所述进一步冷却了的流被引导进入第一蒸馏塔并在所述较低压力下分馏,由此回收所述挥发性相对较低的馏分的所述组分;
其中改进之处在于,所述气流被充分冷却而得以部分冷凝;以及
(1)所述部分冷凝了的气流被分离,从而提供蒸气流和至少一股液体流;
(2)所述蒸气流被膨胀至所述较低压力并且供应至所述第一蒸馏塔的塔中部进料位置;
(3)所述至少一股液体流的至少一部分被膨胀至所述较低压力并且供应至所述第一蒸馏塔的塔中下部进料位置,其低于所述塔中部进料位置;
(4)从所述第一蒸馏塔的低于所述塔中部进料位置且高于所述塔中下部进料位置的区域抽取蒸馏液体流;
(5)所述蒸馏液体流被加热,并且随后被引导进入第二蒸馏塔并且分馏成为顶部蒸气流和底部液体流;
(6)所述顶部蒸气流被冷却以实质上全部冷凝,从而形成冷凝流;
(7)所述冷凝流被分成第一部分和第二部分,由此所述第一部分被引导至所述第二蒸馏塔的顶部进料位置;
(8)所述第二部分被引导至所述第一蒸馏塔的塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域;
(9)所述底部液体流被冷却,从而供应步骤(5)的至少一部分加热作用;
(10)所述冷却了的底部液体流被引导至所述第一蒸馏塔的顶部进料位置;
(11)进入所述第二蒸馏塔的所述进料流的量和温度有效地将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(12)进入所述第一蒸馏塔的所述进料流的量和温度有效地将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
3.一种用于分离气流的工艺,其中包含甲烷和更易挥发组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述工艺中:
(a)所述气流在带压下被冷却以提供冷却流;
(b)所述冷却流被膨胀至较低压力,从而进一步被冷却;以及
(c)所述进一步冷却了的流被引导进入第一蒸馏塔并在所述较低压力下分馏,由此回收所述挥发性相对较低的馏分的所述组分;
其中改进之处在于,冷却之后,所述冷却流被分成第一股和第二股流;以及
(1)所述第二股流被膨胀至所述较低压力并且供应至所述第一蒸馏塔的塔中部进料位置;
(2)从所述第一蒸馏塔的低于所述塔中部进料位置的区域抽取蒸馏液体流;
(3)所述蒸馏液体流被加热,并且随后被引导进入第二蒸馏塔并且分馏成为顶部蒸气流和底部液体流;
(4)所述顶部蒸气流被冷却以实质上全部冷凝,从而形成冷凝流;
(5)所述冷凝流被分成第一部分和第二部分,由此所述第一部分被引导至所述第二蒸馏塔的顶部进料位置;
(6)所述第二部分被引导至所述第一蒸馏塔的塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域;
(7)所述底部液体流被冷却,从而供应步骤(3)的至少一部分加热作用;
(8)所述第一股流被膨胀至中度压力并且随后与所述冷却了的底部液体流合并以形成合并流;
(9)所述合并流被冷却并随后膨胀至所述较低压力;
(10)所述膨胀了的冷却合并流被引导至所述第一蒸馏塔的顶部进料位置;
(11)进入所述第二蒸馏塔的所述进料流的量和温度有效地将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(12)进入所述第一蒸馏塔的所述进料流的量和温度有效地将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
4.一种用于分离气流的工艺,其中包含甲烷和更易挥发组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述工艺中:
(a)所述气流在带压下被冷却以提供冷却流;
(b)所述冷却流被膨胀至较低压力,从而进一步被冷却;以及
(c)所述进一步冷却了的流被引导进入第一蒸馏塔并在所述较低压力下分馏,由此回收所述挥发性相对较低的馏分的所述组分;
其中改进之处在于,所述气流被充分冷却而得以部分冷凝;以及
(1)所述部分冷凝了的气流被分离,从而提供蒸气流和至少一股液体流;
(2)所述蒸气流随后被分成第一股和第二股流;
(3)所述第二股流被膨胀至所述较低压力并且供应至所述第一蒸馏塔的塔中部进料位置;
(4)所述至少一股液体流的至少一部分被膨胀至所述较低压力并且供应至所述第一蒸馏塔的塔中下部进料位置,其低于所述塔中部进料位置;
(5)从所述第一蒸馏塔中低于所述塔中部进料位置且高于所述塔中下部进料位置的区域抽取蒸馏液体流;
(6)所述蒸馏液体流被加热,并且随后被引导进入第二蒸馏塔并且分馏成为顶部蒸气流和底部液体流;
(7)所述顶部蒸气流被冷却以实质上全部冷凝,从而形成冷凝流;
(8)所述冷凝流被分成第一部分和第二部分,由此所述第一部分被引导至所述第二蒸馏塔的顶部进料位置;
(9)所述第二部分被引导至所述第一蒸馏塔的塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域;
(10)所述底部液体流被冷却,从而供应步骤(6)的至少一部分加热作用;
(11)所述第一股流被膨胀至中度压力并且随后与所述冷却了的底部液体流合并以形成合并流;
(12)所述合并流被冷却并随后膨胀至所述较低压力;
(13)所述膨胀了的冷却合并流被引导至所述第一蒸馏塔的顶部进料位置;
(14)进入所述第二蒸馏塔的所述进料流的量和温度有效地将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(15)进入所述第一蒸馏塔的所述进料流的量和温度有效地将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
5.根据权利要求2或4所述的改进,其中所述至少一股液体流的所述膨胀了的至少一部分被加热并且随后供应至所述第一蒸馏塔的所述塔中下部进料位置,其低于所述塔中部进料位置。
6.根据权利要求1、2、3或4所述的改进,其中
(1)所述顶部蒸气流被充分冷却而得以部分冷凝;
(2)所述部分冷凝了的顶部蒸气流被分离,从而提供残余蒸气流和所述冷凝流;以及
(3)所述残余蒸气流被引导至所述第一蒸馏塔的第二个塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域。
7.根据权利要求5所述的改进,其中
(1)所述顶部蒸气流被充分冷却而得以部分冷凝;
(2)所述部分冷凝了的顶部蒸气流被分离,从而提供残余蒸气流和所述冷凝流;以及
(3)所述残余蒸气流被引导至所述第一蒸馏塔的第二个塔下部进料位置,其低于从所述第一蒸馏塔中抽取所述蒸馏液体流的所述区域。
8.一种用于分离气流的设备,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述设备中具有
(a)冷却在带压下的所述气流的第一冷却构件,其被连接以提供在带压下的冷却流;
(b)膨胀构件,其被连接以接收在带压下的所述冷却流的至少一部分并将它膨胀至较低压力,由此所述流被进一步冷却;以及
(c)第一蒸馏塔,其被连接以接收所述进一步冷却了的流,所述第一蒸馏塔被调适以将所述进一步冷却了的流分离成所述挥发性残余气体馏分和所述挥发性相对较低的馏分;
其中改进之处在于,所述进一步冷却了的膨胀流被引导至所述第一蒸馏塔的塔中部进料位置;以及所述设备包括
(1)液体抽取构件,其连接于所述第一蒸馏塔以接收来自所述第一蒸馏塔的低于所述塔中部进料位置的区域的蒸馏液体流;
(2)热交换构件,其连接于所述液体抽取构件以接收所述蒸馏液体流并对它加热;
(3)第二蒸馏塔,其连接于所述热交换构件以接收所述加热了的蒸馏液体流并且将它分馏成顶部蒸气流和底部液体流;
(4)第二冷却构件,其连接于所述第二蒸馏塔以接收所述顶部蒸气流并且将它充分冷却以使其实质上冷凝,从而形成冷凝流;
(5)分隔构件,其连接于所述第二冷却构件以接收所述冷凝流并且将它至少分为第一部分和第二部分;
(6)所述分隔构件连接于所述第二蒸馏塔以将所述第一部分供应至所述第二蒸馏塔的顶部进料位置;
(7)所述分隔构件还连接于所述第一蒸馏塔以将所述第二部分供应至所述第一蒸馏塔的塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域;
(8)所述热交换构件还连接于所述第二蒸馏塔以接收所述底部液体流并将它冷却,从而供应步骤(2)的至少一部分加热作用;所述热交换构件还被连接于所述第一蒸馏塔以将所述冷却了的底部液体流供应至所述第一蒸馏塔的顶部进料位置;
(9)第一控制构件,其被调适以调控进入所述第二蒸馏塔的所述进料流的量和温度以将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(10)第二控制构件,其被调适以调控进入所述第一蒸馏塔的所述进料流的量和温度以将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
9.一种用于分离气流的设备,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述设备中具有:
(a)冷却在带压下的所述气流的第一冷却构件,其被连接以提供在带压下的冷却流;
(b)第一膨胀构件,其被连接以接收在带压下的所述冷却流的至少一部分并将它膨胀至较低压力,由此所述流被进一步冷却;以及
(c)第一蒸馏塔,其被连接以接收所述进一步冷却了的流,所述第一蒸馏塔被调适以将所述进一步冷却了的流分离成所述挥发性残余气体馏分和所述挥发性相对较低的馏分;
其中改进之处在于,所述设备包括
(1)所述第一冷却构件,其被调适以充分冷却在带压下的所述气流以使它部分冷凝;
(2)分离构件,其连接于所述第一冷却构件以接收所述部分冷凝了的气流并且将它分离成蒸气流和至少一股液体流;
(3)所述第一膨胀构件,其连接于所述分离构件以接收所述蒸气流并且将它膨胀至所述较低压力,所述第一膨胀构件还被连接于所述第一蒸馏塔以将所述膨胀了的蒸气流供应至所述第一蒸馏塔的塔中部进料位置;
(4)第二膨胀构件,其连接于所述分离构件以接收所述至少一股液体流的至少一部分并且将它膨胀至所述较低压力,所述第二膨胀构件还被连接于所述第一蒸馏塔以将所述膨胀了的液体流供应至所述第一蒸馏塔的塔中下部进料位置,其低于所述塔中部进料位置;
(5)液体抽取构件,其连接于所述第一蒸馏塔以接收来自所述第一蒸馏塔的低于所述塔中部进料位置并且高于所述塔中下部进料位置的区域的蒸馏液体流;
(6)热交换构件,其连接于所述液体抽取构件以接收所述蒸馏液体流并对它加热;
(7)第二蒸馏塔,其连接于所述热交换构件以接收所述加热了的蒸馏液体流并且将它分馏成顶部蒸气流和底部液体流;
(8)第二冷却构件,其连接于所述第二蒸馏塔以接收所述顶部蒸气流并且将它充分冷却以使其实质上冷凝,从而形成冷凝流;
(9)分隔构件,其连接于所述第二冷却构件以接收所述冷凝流并且将它至少分为第一部分和第二部分;
(10)所述分隔构件连接于所述第二蒸馏塔以将所述第一部分供应至所述第二蒸馏塔的顶部进料位置;
(11)所述分隔构件还连接于所述第一蒸馏塔以将所述第二部分供应至所述第一蒸馏塔的塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域;
(12)所述热交换构件还连接于所述第二蒸馏塔以接收所述底部液体流并将它冷却,从而供应步骤(6)的至少一部分加热作用,所述热交换构件还被连接于所述第一蒸馏塔以将所述冷却了的底部液体流供应至所述第一蒸馏塔的顶部进料位置;
(13)第一控制构件,其被调试以调控进入所述第二蒸馏塔的所述进料流的量和温度以将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(14)第二控制构件,其被调试以调控进入所述第一蒸馏塔的所述进料流的量和温度以将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
10.一种用于分离气流的设备,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述设备中具有
(a)冷却在带压下的所述气流的第一冷却构件,其被连接以提供在带压下的冷却流;
(b)第一膨胀构件,其被连接以接收在带压下的所述冷却流的至少一部分并将它膨胀至较低压力,由此所述流被进一步冷却;以及
(c)第一蒸馏塔,其被连接以接收所述进一步冷却了的流,所述第一蒸馏塔被调适以将所述进一步冷却了的流分离成所述挥发性残余气体馏分和所述挥发性相对较低的馏分;
其中改进之处在于,所述设备包括
(1)第一分隔构件,其连接于所述第一冷却构件以接收所述冷却流并且将它分为第一股和第二股流;
(2)所述第一膨胀构件,其连接于所述第一分隔构件以接收所述第二股流并且将它膨胀至所述较低压力,所述第一膨胀构件还被连接于所述第一蒸馏塔以将所述膨胀了的第二股流供应至所述第一蒸馏塔的塔中部进料位置;
(3)液体抽取构件,其连接于所述第一蒸馏塔以接收来自所述第一蒸馏塔的低于所述塔中部进料位置的区域的蒸馏液体流;
(4)热交换构件,其连接于所述液体抽取构件以接收所述蒸馏液体流并对它加热;
(5)第二蒸馏塔,其连接于所述热交换构件以接收所述加热了的蒸馏液体流并且将它分馏成顶部蒸气流和底部液体流;
(6)第二冷却构件,其连接于所述第二蒸馏塔以接收所述顶部蒸气流并且将它充分冷却以使其实质上冷凝,从而形成冷凝流;
(7)第二分隔构件,其连接于所述第二冷却构件以接收所述冷凝流并且将它至少分为第一部分和第二部分;
(8)所述第二分隔构件连接于所述第二蒸馏塔以将所述第一部分供应至所述第二蒸馏塔的顶部进料位置;
(9)所述第二分隔构件还连接于所述第一蒸馏塔以将所述第二部分供应至所述第一蒸馏塔的塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域;
(10)所述热交换构件还连接于所述第二蒸馏塔以接收所述底部液体流并将它冷却,从而供应步骤(4)的至少一部分加热作用;
(11)第二膨胀构件,其连接于所述第一分隔构件以接收所述第一股流并且将它膨胀至中度压力;
(12)合并构件,其连接于所述第二膨胀构件和所述热交换构件以接收所述膨胀了的第一股流和所述冷却了的底部液体流并且形成合并流;
(13)第三冷却构件,其连接于所述合并构件以接收所述合并流并且将它冷却;
(14)第三膨胀构件,其连接于所述第三冷却构件以接收所述冷却了的合并流并且将它膨胀至所述较低压力,所述第三膨胀构件还连接于所述第一蒸馏塔以将所述膨胀了的冷却合并流供应至所述第一蒸馏塔的顶部进料位置;
(15)第一控制构件,其被调试以调控进入所述第二蒸馏塔的所述进料流的量和温度以将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(16)第二控制构件,其被调试以调控进入所述第一蒸馏塔的所述进料流的量和温度以将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
11.一种用于分离气流的设备,其中包含甲烷和更易挥发的组分、C2组分、C3组分和重烃组分的气流被分离成挥发性残余气体馏分和包含大部分所述C2组分、C3组分和重烃组分的挥发性相对较低的馏分,在所述设备中具有:
(a)冷却在带压下的所述气流的第一冷却构件,其被连接以提供在带压下的冷却流;
(b)第一膨胀构件,其被连接以接收在带压下的所述冷却流的至少一部分并将它膨胀至较低压力,由此所述流被进一步冷却;以及
(c)第一蒸馏塔,其被连接以接收所述进一步冷却了的流,所述第一蒸馏塔被调适以将所述进一步冷却了的流分离成所述挥发性残余气体馏分和所述挥发性相对较低的馏分;
其中改进之处在于,所述设备包括
(1)所述第一冷却构件,其被调适以充分冷却在带压下的所述气流以使它部分冷凝;
(2)分离构件,其连接于所述第一冷却构件以接收所述部分冷凝了的气流并且将它分离成蒸气流和至少一股液体流;
(3)第一分隔构件,其连接于所述分离构件以接收所述蒸气流并且将它分为第一股和第二股流;
(4)所述第一膨胀构件,其连接于所述第一分隔构件以接收所述第二股流并且将它膨胀至所述较低压力,所述第一膨胀构件还被连接于所述第一蒸馏塔以将所述膨胀了的第二股流供应至所述第一蒸馏塔的塔中部进料位置;
(5)第二膨胀构件,其连接于所述分离构件以接收所述至少一股液体流的至少一部分并且将它膨胀至所述较低压力,所述第二膨胀构件还连接于所述第一蒸馏塔以将所述膨胀了的液体流供应至所述第一蒸馏塔的塔中下部进料位置,其低于所述塔中部进料位置;
(6)液体抽取构件,其连接于所述第一蒸馏塔以接收来自所述第一蒸馏塔的低于所述塔中部进料位置并且高于所述塔中下部进料位置的区域的蒸馏液体流;
(7)热交换构件,其连接于所述液体抽取构件以接收所述蒸馏液体流并对它加热;
(8)第二蒸馏塔,其连接于所述热交换构件以接收所述加热了的蒸馏液体流并且将它分馏成顶部蒸气流和底部液体流;
(9)第二冷却构件,其连接于所述第二蒸馏塔以接收所述顶部蒸气流并且将它充分冷却以使其实质上冷凝,从而形成冷凝流;
(10)第二分隔构件,其连接于所述第二冷却构件以接收所述冷凝流并且将它至少分为第一部分和第二部分;
(11)所述第二分隔构件连接于所述第二蒸馏塔以将所述第一部分供应至所述第二蒸馏塔的顶部进料位置;
(12)所述第二分隔构件还连接于所述第一蒸馏塔以将所述第二部分供应至所述第一蒸馏塔的塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域;
(13)所述热交换构件还连接于所述第二蒸馏塔以接收所述底部液体流并将它冷却,从而供应步骤(7)的至少一部分加热作用;
(14)第三膨胀构件,其连接于所述第一分隔构件以接收所述第一股流并且将它膨胀至中度压力;
(15)合并构件,其连接于所述第三膨胀构件和所述热交换构件以接收所述膨胀了的第一股流和所述冷却了的底部液体流并且形成合并流;
(16)第三冷却构件,其连接于所述合并构件以接收所述合并流并将它冷却;
(17)第四膨胀构件,其连接于所述第三冷却构件以接收所述冷却了的合并流并且将它膨胀至所述较低压力,所述第四膨胀构件还连接于所述第一蒸馏塔以将所述膨胀了的冷却合并流供应至所述第一蒸馏塔的顶部进料位置;
(18)第一控制构件,其被调试以调控进入所述第二蒸馏塔的所述进料流的量和温度以将所述第二蒸馏塔的顶部温度维持于一定温度,由此使得所述顶部蒸气流主要为C3烃组分和更易挥发的组分,并且所述底部液体流主要为C4-C5烃组分;以及
(19)第二控制构件,其被调试以调控进入所述第一蒸馏塔的所述进料流的量和温度以将所述第一蒸馏塔的顶部温度维持于一定温度,由此使得所述挥发性相对较低的馏分中的所述大部分组分得以回收。
12.根据权利要求8所述的改进,其中
(1)所述第二冷却构件被调适以将所述顶部蒸气流充分冷却而使其部分冷凝;
(2)分离构件连接于所述第二冷却构件以接收所述部分冷凝了的顶部蒸气流并且将它分离成残余蒸气流和所述冷凝流;
(3)所述分隔构件被调适以连接于所述分离构件,用以接收所述冷凝流;以及
(4)所述分离构件连接于所述第一蒸馏塔以将所述残余蒸气流供应至所述第一蒸馏塔的第二个塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域。
13.根据权利要求9所述的改进,其中
(1)所述第二冷却构件被调适以将所述顶部蒸气流充分冷却而使其部分冷凝;
(2)第二分离构件连接于所述第二冷却构件以接收所述部分冷凝了的顶部蒸气流并且将它分离成残余蒸气流和所述冷凝流;
(3)所述分隔构件被调适以连接于所述第二分离构件,用以接收所述冷凝流;以及
(4)所述第二分离构件连接于所述第一蒸馏塔以将所述残余蒸气流供应至所述第一蒸馏塔的第二个塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域。
14.根据权利要求10所述的改进,其中
(1)所述第二冷却构件被调适以将所述顶部蒸气流充分冷却而使其部分冷凝;
(2)分离构件连接于所述第二冷却构件以接收所述部分冷凝了的顶部蒸气流并且将它分离成残余蒸气流和所述冷凝流;
(3)所述第二分隔构件被调适以连接于所述分离构件,用以接收所述冷凝流;以及
(4)所述分离构件连接于所述第一蒸馏塔以将所述残余蒸气流供应至所述第一蒸馏塔的第二个塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域。
15.根据权利要求11所述的改进,其中
(1)所述第二冷却构件被调适以将所述顶部蒸气流充分冷却而使其部分冷凝;
(2)第二分离构件连接于所述第二冷却构件以接收所述部分冷凝了的顶部蒸气流并且将它分离成残余蒸气流和所述冷凝流;
(3)所述第二分隔构件被调适以连接于所述第二分离构件,用以接收所述冷凝流;以及
(4)所述第二分离构件连接于所述第一蒸馏塔以将所述残余蒸气流供应至所述第一蒸馏塔的第二个塔下部进料位置,其低于所述液体抽取构件连接于所述第一蒸馏塔以抽取所述蒸馏液体流的所述区域。
16.根据权利要求9、11、13或15所述的改进,其中加热构件连接于所述第二膨胀构件以接收所述膨胀了的液体流并且对它加热,所述加热构件还连接于所述第一蒸馏塔以将所述加热了的膨胀液体流供应至所述第一蒸馏塔的所述塔中下部进料位置。
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CA2786487C (en) | 2017-08-01 |
EA021836B1 (ru) | 2015-09-30 |
ZA201205795B (en) | 2013-05-29 |
CA2786487A1 (en) | 2011-07-21 |
MX2012008087A (es) | 2012-12-17 |
JP5798127B2 (ja) | 2015-10-21 |
AR079908A1 (es) | 2012-02-29 |
KR101660082B1 (ko) | 2016-09-26 |
AU2010341438A1 (en) | 2012-08-23 |
BR112012017390A2 (pt) | 2016-04-19 |
UA109428C2 (uk) | 2015-08-25 |
MY158951A (en) | 2016-11-30 |
SA111320085B1 (ar) | 2014-09-15 |
SG182389A1 (en) | 2012-08-30 |
US20110167868A1 (en) | 2011-07-14 |
EA201201013A1 (ru) | 2012-12-28 |
CL2012001837A1 (es) | 2012-11-16 |
US9021832B2 (en) | 2015-05-05 |
KR20120104633A (ko) | 2012-09-21 |
WO2011087884A1 (en) | 2011-07-21 |
CO6571915A2 (es) | 2012-11-30 |
EP2524181A1 (en) | 2012-11-21 |
PE20130058A1 (es) | 2013-02-04 |
JP2013517450A (ja) | 2013-05-16 |
CN102741634B (zh) | 2015-06-03 |
NZ601500A (en) | 2014-08-29 |
AU2010341438B2 (en) | 2015-01-29 |
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