CN113454411A - 具有混合制冷剂冷却的脱氢分离装置 - Google Patents

具有混合制冷剂冷却的脱氢分离装置 Download PDF

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CN113454411A
CN113454411A CN201980066720.9A CN201980066720A CN113454411A CN 113454411 A CN113454411 A CN 113454411A CN 201980066720 A CN201980066720 A CN 201980066720A CN 113454411 A CN113454411 A CN 113454411A
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primary
heat exchanger
fluid communication
outlet
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D.A.小杜科特
B.A.海尔曼
T.P.古沙纳斯
R.霍普韦尔
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Chart Energy and Chemicals Inc
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Chart Energy and Chemicals Inc
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Priority to CN202210528229.7A priority Critical patent/CN115127303A/zh
Priority to CN202311338862.0A priority patent/CN118009629A/zh
Publication of CN113454411A publication Critical patent/CN113454411A/zh
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Abstract

用于分离来自脱氢反应器的流出液流中的烯烃和氢气的系统，包括热交换器，该热交换器接收并部分地冷凝流出液流，从而形成混合相流出液流。初级分离装置接收并将混合相流出流分离成初级蒸汽流和初级液体产品流。热交换器接收并部分地冷凝初级蒸汽流，从而形成混合相初级流。二次分离装置接收混合相初级流并将该混合相初级流分离成二次蒸汽流和二次液体产品流。热交换器接收并加热二次蒸汽流以提供用于部分地冷凝流出液流的制冷，热交换器接收并加热二次蒸汽流以提供用于部分地冷凝初级蒸汽流的制冷。混合制冷剂压缩系统向热交换器提供制冷剂以提供制冷。

Description

具有混合制冷剂冷却的脱氢分离装置
优先权要求
本申请要求于2018年10月9日提交的美国临时专利申请第62/743,263号的优先权权益，其内容通过引用并入本文。
背景技术
丙烷脱氢(PDH)分离系统是本领域已知的。在共同拥有的美国专利第6,333,445号中描述了这种系统的一个示例，其内容通过引用并入本文。
目前PDH分离系统的设计要求使用反应器流出物压缩机将反应器流出物蒸汽流压缩到高压(～12Barg)，然后使用两个发电机制动或压缩机制动的低温涡轮膨胀机将其减压，从而提供用于分离和回收液体烯烃产品所需的制冷。
这样的现有技术系统的缺点包括整个过程的功率消耗、涡轮膨胀机/发电机(或压缩机)组的增加的成本和维护要求、高要求的反应器流出物压缩机排放压力(这增加了资金和操作成本)以及缺乏显著调节烯烃和氢气分离温度的灵活性。
发明内容
本发明主题的几个方面可以在下面描述和要求保护的设备和系统中单独或一起实施。这些方面可以单独使用，也可以与本文所述主题的其它方面结合使用，这些方面的描述在一起并不旨在排除这些方面的单独使用或这些方面的单独要求或如所附权利要求书中所述的不同组合。
一方面，用于分离来自脱氢反应器的流出液流中的烯烃和氢气的系统包括主热交换器，该主热交换器被配置为接收并部分地冷凝流出液流，从而形成混合相流出流。初级分离装置与主热交换器成流体连通，以接收混合相流出流并将其分离成初级蒸汽流和初级液体产品流。主热交换器被配置为接收并部分地冷凝初级蒸汽流，从而形成混合相初级流。二次分离装置与主热交换器成流体连通，以接收混合相初级流并将其分离成二次蒸汽流和二次液体产品流。主热交换器被配置为接收并加热二次蒸汽流以提供用于部分地冷凝流出液流和初级蒸汽流的制冷。混合制冷剂压缩系统被配置为也向主热交换器提供制冷剂。
另一方面，用于分离来自脱氢反应器的流出液流中的烯烃和氢气的系统包括冷箱进料热交换器，该冷箱进料热交换器被配置为接收并部分地冷凝流出液流，从而形成混合相流出流。初级分离装置与冷箱进料热交换器成流体连通，以接收混合相流出流并将其分离成初级蒸汽流和初级液体产品流。混合制冷剂热交换器被配置为接收并部分地冷凝初级蒸汽流，从而形成混合相初级流。二次分离装置与混合制冷剂热交换器成流体连通，以接收混合相初级流并将其分离为二次蒸汽流和二次液体产品流。混合制冷剂热交换器被配置为接收和加热二次蒸汽流，以提供用于部分地冷凝初级蒸汽流的制冷。冷箱进料换热器被配置为接收并进一步加热离开混合制冷剂热交换器后的二次蒸汽流，以提供用于部分地冷凝流出液流的制冷。混合制冷剂压缩系统被配置为向混合制冷剂热交换器提供制冷剂。
又一方面，分离来自脱氢反应器的流出液流中的烯烃和氢气的方法包括以下步骤：部分地冷凝流出液流以形成混合相流出流，将混合相流出流分离成初级蒸汽流和初级液体产品流，部分地冷凝初级蒸汽流以形成混合相初级蒸汽流，将混合相初级流分离成二次蒸汽流和二次液体产品流，加热二次蒸汽流以提供用于部分地冷凝流出液流和初级蒸汽流的制冷，并从混合制冷剂压缩系统向主热交换器提供制冷剂。
附图说明
图1是本公开的系统的第一实施方式的示意图；
图2是本公开的系统的第二实施方式的示意图；
图3是本公开的系统的第三实施方式的示意图；
图4是本公开的系统的第四实施方式的示意图；
图5是本公开的系统的第五实施方式的示意图。
具体实施方式
本发明是脱氢分离装置，其中使用混合制冷剂(MR)系统来提供分离和回收液体烯烃产品所需的制冷，所述MR系统由具有热交换器和鼓的MR压缩机组成。仅作为示例，MR系统可以使用单个混合制冷剂系统，或者是使用第二制冷剂预冷却的单个混合制冷剂系统。
在实现与现有技术系统相同的产品回收率的同时，一些益处可以包括：1)整个工艺的能耗较低，2)省去了涡轮膨胀机/发电机(或压缩机)两套机组，3)所需的反应器流出物压缩机排放压力显著降低，节约了资金和运行费用，4)与涡轮膨胀机工艺相比，MR工艺改善了分离系统的操作、维护和可靠性，5)MR工艺允许主进料热交换器的更强健和更耐用的设计，6)MR工艺提供了独立的装置来调节分离系统的制冷水平，而不影响循环流出物压缩机。
由于在许多PDH设备中使用丙烯制冷，因此本文所述的MR工艺使用丙烯制冷来预冷MR制冷剂并降低MR压缩机功耗。预冷还允许简化MR组分混合物，只需要甲烷、乙烯(或乙烷)和丙烯(或丙烷)，优选乙烯和丙烯。在MR混合物中没有C4或C5，降低了反应器催化剂污染的可能性。
虽然下面给出的本发明的解释是针对丙烷脱氢装置，但是对于丁烷脱氢也可以使用相同的工艺。
参照图1，反应器流出气体在REC压缩机中被压缩到约7.2巴，并且在压缩热作为冷箱蒸气进料8进入低温分离系统之前将其去除。气体被送往冷箱进料热交换器9，在那里它被部分地冷凝，然后流向出口初级分离器10。蒸汽和液体被分离，其中液体流含有一部分C3烯烃产品，蒸汽流17含有氢气和剩余烯烃产品。
该蒸汽流17流向混合制冷剂热交换器11(MR交换器)，在那里它被进一步冷却到所需温度并部分地冷凝以实现所需的产品回收率。部分地冷凝的流流向二次分离器12，并被分离成液体烯烃产品和富氢蒸汽流21。富氢流在MR交换器中再加热，然后分成两股物流-循环气13(这是组合反应器进料所需的氢)和净蒸汽16(其是氢气物流的余量，并将从分离系统中输出。
在新鲜进料热交换器(具有冷端26和热端32)中再加热净蒸汽流并回收制冷。液体产品流(来自初级和二次分离器10和12)组合以形成组合的液体产品流18，并流向新鲜进料热交换器26,32。
冷箱蒸汽进料8(“反应器流出物”)首先在冷箱进料交换器中冷却。其通过组合的反应器进料14初步冷却，并且通过输出净蒸汽产品16的一部分24二次冷却。通过将循环气流13与冷的新鲜进料液流15(如丙烷或正丁烷)组合并在冷箱进料热交换器9中蒸发该组合流，组合的反应器进料提供了大部分的制冷。冷的新鲜进料液体流15由新鲜进料入口流23形成，该新鲜进料入口流23在进入冷箱进料热交换器9之前在新鲜进料热交换器中在26和32处被过冷(sub-cooled)。通过从C3烯烃产品18和从净蒸汽产品16的一部分回收冷量来提供新鲜进料的制冷。
闪蒸气体(再循环)19是通过部分地加热新鲜进料交换器的冷端部分26中的分离器液体而产生的。在液体产品罐28中分离得到的汽-液混合物27。来自罐28的蒸汽在新鲜进料交换器的热端部分32中被加热，闪蒸气体19再循环到上游的反应器流出物压缩机的吸入部(参见美国专利No.6,333,445的图1)。来自罐28的液体产品经由泵34被泵送，并且在新鲜进料交换器的暖端部分32中回收附加的冷量。
分离系统的总制冷平衡由混合制冷剂(MR)压缩系统(在图1中一般用38表示)经由MR交换器(MRHX)11中的最终冷却来)。本文描述了一种C3预冷却MR系统；然而，也可以使用单个MR系统。图1示出了单级MR压缩机40，接着是空气或水冷却器42，然后是C3(丙烯)预冷却器44。预冷却器可以根据需要利用尽可能多的制冷级来获得所需的温度，为了简化，示出了两个级。MR制冷剂经由分离器46分别分离成汽相流和液相流31和33，并被送往MRHX 11。MR蒸汽流31在MRHX 11中冷却和冷凝，并在35闪蒸以产生用于该工艺的最冷制冷剂和低压制冷剂流37。MR液体流33也在MRHX中被冷却，在41闪蒸并被送往低压制冷剂流37，在那里其与低压制冷剂流37在较热的温度下汇合并混合。共用制冷剂返回流47作为混合相蒸汽/液体流离开MRHX。在压缩之前，蒸汽和液体经由分离器48分离。液体经由泵49被泵浦到较高的压力，蒸汽在压缩机40被压缩到所需的排放压力。该系统使用适合于特定设计条件的典型MR组合物。
图1所示和上面所述的热交换器可以加入或集成到单个主热交换器中。
参照图2，在系统的第二实施方式中，MR压缩机的吸入鼓也可以被设计成用作重组分制冷剂蓄积器。MR系统可以用在制冷剂中的过量的重组分(诸如C3、C4或C5)来操作，所得到的MR至少暂时是离开交换器11的两相流52。这些过量的重组分在压缩机吸入鼓50中被分离并保留在鼓中。流向MR压缩机40的制冷剂蒸汽现在处于其露点，并且该系统在露点条件下自动操作。当“补充”制冷剂被加入到系统时，累积的重组分随后将在吸入压力和温度下与轻组分平衡至露点。如果需要，可以优选在吸入蓄积器处从制冷系统去除重组分或者优选将重组分添加并保持在吸入鼓中。
在系统的第三实施方式中，如图3所示，反应器流出气体在REC压缩机中被压缩到约7.2巴，压缩热在作为冷箱蒸汽进料108进入低温分离系统之前经由环境交换器(空气或水)冷却而被除去。气体被送往主热交换器110，在那里其被冷却和部分地冷凝，然后流向初级分离器112。分离蒸汽和液体，液体流114含有部分C3烯烃产品，蒸汽流116含有氢和剩余的烯烃产品。该蒸汽流流回到主热交换器110，在那里其被进一步冷却和部分地冷凝以实现所需的产品回收。部分地冷凝的物流118流向二次分离器122，并被分离成液体烯烃产品124和富氢流126。富氢蒸汽流在主热交换器中再加热，然后在130被分成两股流-循环气132(其是组合反应器进料133所需的氢气)和净蒸汽134(其是氢气流的余量，并将被从分离系统输出)。净蒸汽流被再加热并在主热交换器中回收制冷。
将加热的新鲜丙烷进料138送往主热交换器110，并冷却到与初级分离器112相同的温度。然后将冷却的新鲜丙烷进料142与循环气132混合以形成组合的反应器进料133。该物流被再加热，并且在主热交换器中回收制冷。这为低温分离系统提供了大多数的制冷。
液体产品流114和124(来自初级分离器和二次分离器112和122)在与它们各自的温度相关的适当位置被送入主热交换器110。液体产品流被加热，并部分汽化。液体产品流通过共用集流管离开主热交换器，形成液体产品流146。液体产品流的这种取向提高了效率，降低了管道复杂性，并降低了冻结的风险。
将部分汽化的混合C3液体产品流146送往液体产品罐150。来自液体产品罐的蒸汽152(闪蒸气体)在主热交换器中被加热，然后作为闪蒸气流154再循环到上游的反应器流出物压缩机的吸入部。来自液体产品罐的液体156(液体产品)经由泵158泵送，然后在主热交换器中加热以用于附加的能量回收。加热的液体产品作为C3产品流162离开主热交换器。
分离系统的总制冷平衡由通常用168表示的混合制冷剂(MR)系统提供。图3的实施方式使用两级MR压缩机172，具有空气或水的中间冷却和排放冷却。第一MR压缩机级的排出物174在175处部分地冷凝，并被送往MR级间鼓176。蒸气178被送往第二MR压缩机级，液体182被送往主热交换器110。第二MR压缩机级排出物184在185部分地冷凝，并在MR蓄积器186中分离。MR蓄积器蒸汽192和液体194被送往主热交换器110。MR蓄积器蒸汽在主热交换器中被部分地冷凝，并且产生的流196被送往冷蒸汽分离器鼓202以提高工艺效率。冷蒸汽分离器蒸汽204、冷蒸汽分离器液体206、MR蓄积器液体194和MR级间液体182都在主热交换器110中冷凝和过冷(sub-cooled)。所有这些流都离开交换器，通过JT阀(仅作为示例)闪蒸，分离得到的混合相流，并在适当的温度下经由竖管212、213、214和216送回主热交换器，以提供分离系统所需的制冷余量。关于MR系统168的操作的其它细节可见Ducote,Jr.等人的共同拥有的美国专利申请公开第US2014/0260415号，其全部内容通过引用并入本文。
闪蒸的低压MR流在主热交换器内混合，并作为单个过热蒸汽流220离开，该蒸汽流被送往MR压缩机吸入鼓224。该系统使用适合于特定设计条件的典型MR组合物。
MR系统允许将处于环境温度或更冷的附加热传递服务集成到主热交换器中。作为示例，图3示出了脱乙烷塔精馏冷凝器(脱乙烷塔塔顶入口流226和脱乙烷塔塔顶出口流228)与主热交换器的集成。这增加了MR系统的尺寸，因为需要额外的制冷负载，但是去除了用于脱乙烷塔精馏冷凝器服务的单独的C3制冷系统的需求，这减少了脱氢厂的总设备数。
在本公开的系统的第四实施方式中，如图4所示，级间分离装置406被加入到图1的系统中。来自MR热交换器11的混合相MR流402(其在进入MR热交换器之前作为分离器46的液体排出产生)与来自压缩机40的第一级排出的混合相MR流404组合。组合的流被导向分离装置406的入口，而得到的蒸汽流408被导向压缩机40的第二级的入口。第二级压缩机40的排出被导向冷却装置42和44，然后MR流的处理如以上参照图1所述地继续进行，不同之处在于流33在混合制冷剂热交换器11中冷却并经由阀41闪蒸之后不与低压制冷剂流37汇合。然而，在可替代的实施方式中，流33的一部分在于混合制冷剂热交换器11中冷却并经由阀41闪蒸之后可以与低压制冷剂流37汇合。
在本公开的系统的第五实施方式中，如图5所示，级间分离装置506被加入到图2的系统中。来自MR热交换器11的混合相MR流502与来自MR压缩机第一级出口的混合相MR流504组合。组合的流被导向分离装置506的入口，产生的蒸汽流508被导向MR压缩机的第二级的入口。MR压缩机的第二级的排出被导向一个或多个冷却装置，然后，MR流的处理继续进行，如以上参照图4所述。
可以将说明书中涉及的热交换器与多流式热交换器的使用，诸如钎焊铝板翅式换热器相结合，以简化管道设计、设备布局或性能。结合的示例可以是新鲜进料-1交换器与新鲜进料-2交换器，或两个新鲜进料交换器与冷箱进料交换器。也可能需要其它的组合。
虽然已经示出和描述了本发明的优选实施方式，但是对于本领域技术人员来说显而易见的是，在不脱离本发明的范围的情况下，可以对其进行改变和修改。

Claims (20)

1.用于分离来自脱氢反应器的流出液流中的烯烃和氢气的系统，包括：
a.主热交换器，所述主热交换器被配置为接收并部分地冷凝流出液流，从而形成混合相流出流；
b.初级分离装置，所述初级分离装置与所述主热交换器成流体连通，以接收所述混合相流出流并将该混合相流出流分离成初级蒸汽流和初级液体产品流；
c.所述主热交换器被配置为接收所述初级蒸汽流并部分地冷凝该初级蒸汽流，从而形成混合相初级流；
d.二次分离装置，所述二次分离装置与所述主热交换器成流体连通，以接收所述混合相初级流并将该混合相初级流分离成二次蒸汽流和二次液体产品流；
e.所述主热交换器被配置为接收所述二次蒸汽流并加热该二次蒸汽流以提供用于部分地冷凝所述流出液流和所述初级蒸汽流的制冷；和
f.混合制冷剂压缩系统，所述混合制冷剂压缩系统被配置为向所述主热交换器提供制冷剂。
2.如权利要求1所述的系统，其中所述主热交换器包括初级制冷通道，所述混合制冷剂压缩系统包括：
i)吸入分离装置，所述吸入分离装置被配置为接受来自所述主热交换器的所述初级制冷通道接收混合相制冷剂流；
ii)压缩机，所述压缩机具有与所述吸入分离装置成流体连通的入口；
iii)冷却装置，所述冷却装置具有与所述压缩机的出口成流体连通的入口；
iv)蓄积器，所述蓄积器具有与所述冷却装置的出口成流体连通的入口和与所述主热交换器的所述初级制冷通道成流体连通的液体出口和蒸汽出口。
3.如权利要求2所述的系统，其中所述冷却装置包括空气或水冷却器及随后的丙烯预冷却器。
4.如权利要求2所述的系统，其中所述主热交换器被配置为部分地冷凝来自所述蓄积器的所述蒸汽出口的蒸气流以形成混合相蓄积器流，并且还包括冷蒸气分离器，所述冷蒸气分离器具有被配置为接收所述混合相蓄积器流的入口，所述冷蒸气分离器具有与所述热交换器的所述初级制冷通道成流体连通的蒸气出口和液体出口。
5.如权利要求4所述的系统，其中所述混合制冷剂压缩系统包括：
i)级间分离装置，所述级间分离装置具有与所述冷却装置成流体连通的入口、与所述热交换器的所述初级制冷通道成流体连通的液体出口和蒸气出口；
ii)压缩机第二级，所述压缩机第二级具有与所述级间分离装置的所述蒸汽出口成流体连通的入口；
iii)第二级冷却装置，所述第二级冷却装置具有与所述压缩机的出口成流体连通的入口和与所述蓄积器成流体连通的出口。
6.如权利要求5所述的系统，其中所述压缩机是包括第一级和第二级的两级压缩机，所述第一级具有与所述吸入分离装置的出口成流体连通的入口和与所述冷却装置成流体连通的出口，所述第二级具有与所述级间分离装置成流体连通的入口和与所述第二级冷却装置成流体连通的出口。
7.如权利要求1所述的系统，还包括结合器，所述结合器被配置为接收并组合来自所述初级分离装置和所述二次分离装置的所述初级液体产品流和所述二次液体产品流，从而形成组合的液体产品流；
并且其中主热交换器包括新鲜进料冷却通道和液体产品通道，所述新鲜进料冷却通道被配置为接收和冷却新鲜进料流，所述液体产品通道被配置为接收并加热所述组合的液体产品流，从而为所述新鲜进料冷却通道提供制冷，所述新鲜进料冷却通道具有出口，所述出口被配置为使得冷却的新鲜进料流被导向和加入所述二次蒸气流。
8.如权利要求7所述的系统，其中所述新鲜进料流主要包含丙烷或主要包含正丁烷。
9.如权利要求7所述的系统，其中所述主热交换器包括：冷箱进料热交换器，所述冷箱进料热交换器被配置为接收并使用来自所述二次蒸气流的制冷以部分地冷凝所述流出物进料流；混合制冷剂热交换器，所述混合制冷剂热交换器被配置为接收所述冷却蒸汽流并使用来自所述混合制冷剂压缩系统的制冷剂冷却所述初级蒸气流；和新鲜进料热交换器，所述新鲜进料热交换器被配置为接收所述新鲜进料流和使用来自所述组合的液体产品流的制冷来冷却所述新鲜进料流。
10.用于分离来自脱氢反应器的流出液流中的烯烃和氢气的系统，包括：
a.冷箱进料热交换器，所述冷箱进料热交换器被配置为接收并部分地冷凝所述流出液流，从而形成混合相流出流；
b.初级分离装置，所述初级分离装置与所述冷箱进料热交换器成流体连通，以接收所述混合相流出流并将该混合相流出流分离成初级蒸汽流和初级液体产品流；
c.混合制冷剂热交换器，所述混合制冷剂热交换器被配置为接收并部分地冷凝所述初级蒸汽流，从而形成混合相初级流；
d.二次分离装置，所述二次分离装置与所述混合制冷剂热交换器成流体连通，以接收所述混合相初级流并将该混合相初级流分离为二次蒸汽流和二次液体产品流；
e.所述混合制冷剂热交换器被配置为接收和加热所述二次蒸汽流，以提供用于部分地冷凝所述初级蒸汽流的制冷；
f.所述冷箱进料换热器被配置为接收并进一步加热离开所述混合制冷剂热交换器后的所述二次蒸汽流，以提供用于部分地冷凝所述流出液流的制冷；和
g.混合制冷剂压缩系统，所述混合制冷剂压缩系统被配置为向所述混合制冷剂热交换器提供制冷剂。
11.如权利要求10所述的系统，其中所述混合制冷剂热交换器包括初级制冷通道，所述混合制冷剂压缩系统包括：
i)吸入分离装置，所述吸入分离装置被配置为从所述混合制冷剂热交换器的所述初级制冷通道接收混合相制冷剂流；
ii)压缩机，所述压缩机具有与所述吸入分离装置成流体连通的入口；
iii)冷却装置，所述冷却装置具有与所述压缩机的出口成流体连通的入口；
iv)蓄积器，所述蓄积器具有与所述冷却装置的出口成流体连通的入口和与所述混合制冷剂热交换器的所述初级制冷通道成流体连通的液体出口和蒸汽出口。
12.如权利要求11所述的系统，其中所述冷却装置包括空气或水冷却器以及随后的丙烯预冷却器。
13.如权利要求11所述的系统，其中所述吸入分离装置包括蒸汽出口和液体出口，所述蒸汽出口与所述压缩机的入口成流体连通，所述吸入分离装置还包含泵，所述泵具有与所述吸入分离装置的所述液体出口成流体连通的泵入口和与所述冷却装置的所述出口成流体连通的泵出口。
14.如权利要求13所述的系统，还包括级间分离装置，并且其中所述压缩机是包括第一级和第二级的两级压缩机，其中所述第一级具有与所述吸入分离装置的所述蒸汽出口成流体连通的入口和与所述级间分离装置的入口成流体连通的出口，并且其中所述第二级具有与所述级间分离装置的出口成流体连通的入口和与所述冷却装置成流体连通的出口，并且其中所述级间分离装置的入口也与所述蓄积器的所述液体出口成流体连通。
15.如权利要求11所述的系统，还包括级间分离装置，并且其中所述压缩机是包括第一级和第二级的两级压缩机，并且其中所述第一级具有与所述吸入分离装置的所述蒸汽出口成流体连通的入口和与所述级间分离装置的入口成流体连通的出口，并且其中所述第二级具有与所述级间分离装置的出口成流体连通的入口和与所述冷却装置成流体连通的出口，并且其中所述级间分离装置的入口也与所述蓄积器的所述液体出口成流体连通。
16.如权利要求10所述的系统，还包括结合器，所述结合器被配置为接收并组合来自所述初级分离装置和所述二次分离装置的所述初级液体产品流和所述二次液体产品流，从而形成组合的液体产品流；
新鲜进料热交换器，所述新鲜进料热交换器包括新鲜进料冷却通道和液体产品通道，所述新鲜进料冷却通道被配置为接收和冷却新鲜进料流，所述液体产品通道被配置为接收并加热所述组合的液体产品流，从而为所述新鲜进料冷却通道提供制冷，所述新鲜进料冷却通道具有出口，该出口被配置为使得冷却的新鲜进料流在进入所述冷箱进料热交换器之前被导向和加入所述二次蒸气流。
17.如权利要求16所述的系统，其中所述新鲜进料流主要包含丙烷或主要包含正丁烷。
18.如权利要求16所述的系统，其中所述冷箱进料热交换器、混合制冷剂热交换器和新鲜进料热交换器被并入到主热交换器中。
19.分离来自脱氢反应器的流出液流中的烯烃和氢气的方法，包括以下步骤：
a.部分地冷凝所述流出液流，从而形成混合相流出流；
b.将所述混合相流出流分离成初级蒸汽流和初级液体产品流；
c.使用混合制冷剂来部分地冷凝所述初级蒸汽流，从而形成混合相初级流；
d.将所述混合相初级流分离成二次蒸汽流和二次液体产品流；和
e.加热所述二次蒸汽流以提供用于部分地冷凝所述流出液流的制冷。
20.如权利要求19所述的方法，还包括以下步骤：
f.组合所述初级液体产品流和所述二次液体产品流以形成组合的液体产品流；
g.通过加热所述组合的液体产品流来冷却所述新鲜进料流，从而形成冷却的新鲜进料流；
h.组合所述冷却的新鲜进料流和所述二次蒸汽流，以形成组合的新鲜进料和二次蒸汽流，所述组合的新鲜进料和二次蒸汽流在步骤e中加热。
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