CN1260541C - 改进的热联合精馏系统 - Google Patents

改进的热联合精馏系统 Download PDF

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CN1260541C
CN1260541C CNB028052145A CN02805214A CN1260541C CN 1260541 C CN1260541 C CN 1260541C CN B028052145 A CNB028052145 A CN B028052145A CN 02805214 A CN02805214 A CN 02805214A CN 1260541 C CN1260541 C CN 1260541C
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大卫·陈
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Abstract

一种改进的热联合精馏系统，其包括一个具有一系列分馏盘的精馏塔，一个位于所述精馏塔上部的回流罐，和一个与该回流罐相连的高架的多制冷剂核心热交换器，以及一个进料系统，其包括一主进料管线，一进料分流装置，该进料分流装置将该主进料管线分为第一进料管线和第二进料管线，第一进料管线包含较少部分的进料，并引入到精馏塔的较低部分，第二进料管线是先通过所述核心热交换器，然后在第一进料管线上方的一高度处进入精馏塔。本发明的系统具有优良的分馏能力，并且所需能量较低。

Description

改进的热联合精馏系统
发明领域
本发明涉及和限定一种相关联的联合的精馏和分馏系统，其共同包括一个用于以最小的能量消耗获得所预定分馏的新颖系统。这个改进的系统包括一个精馏塔，其顶部安装有一个回流罐和一个用于塔进料以及塔顶馏出蒸汽冷却的多制冷剂核心交换器。
发明背景
现在有各种各样的许多公知的用于精馏系统的方法和系统，特别是用于在精馏系统中不同区域和不同步骤中提供和控制热的公知系统。
这些公知的技术包括：McKee的美国专利1,932,903号；Greenwalt的美国专利2,214,790号；Roberts的美国专利2,582,068号；Grossman等人的美国专利3,186,182号；Geddes等人的美国专利3,444,696号；Schramm的美国专利3,555,836号；Pryor等人的美国专利4,002,042号；Rowles等人的美国专利4,270,940号；Bauer的美国专利4,608,068号；Gazzi的美国专利4,657,571号；Coyle等人的美国专利5,505,049号。
McKee的美国专利1,932,903号公开了一种方法，包括以将气体溶解在一种高浓度的有机酸中的方式来液化一种气体，该气体在该高浓度的有机酸中比在水中更易溶解。然后将获得的盐溶液加热以移除溶解的气体，这样重新获得的气体经过使其在精馏器中与液化气体接触而使其干燥，然后将该干燥后的气体冷却。
Greenwalt的美国专利2,214,790号涉及一种分离方法，适用于在至少一两阶段精馏中将一种气体混合物进行分离，精馏的每个阶段都是在不同的超大气压下进行的，使用一种在分离的条件下可以被转化为气态的制冷剂。更具体地说，该方法是特别适用于从气态碳氢混合物中分离乙烯。氨是在气态碳氢混合物中分离组分时选择的制冷剂。
Roberts的美国专利2,582,068号公开了一种用于分离气态混合物的方法和装置，最初是在高压下并回收更多的挥发性组分。该分离方法尤其适用于双组分的气态混合物，以及分离和回收更多的纯的或非常纯化的挥发性组分。
Grossman等人的美国专利3,186,182号公开了一种用于分离气态混合物的低温低压系统和方法，具体地说是用于气体的脱甲烷，以及更具体地说是用于裂化的气态混合物。
Geddes等人的美国专利3,444,696号指出了一种用于气态混合物脱甲烷的改进的方法，为了从含有挥发性比乙烯低或高的组分的气态进料混合物中回收乙烯。该方法包括使冷却的进料混合物经受分馏塔的作用，该分馏塔的顶部具有一个精馏段，其下方具有一个再沸腾汽提(stripping)段，该进料混合物含有乙烯。该发明的方法如所述那样，在经济方面有所改进，如能量消耗，通过在分馏塔段和精馏段以及引入给料处实施精确控制和不同的温度范围，以及通过在分馏塔段使给料与回流之间进行热交换，以除去热。
Schramm的美国专利3,555,836号公开了一种用于分离富乙炔气态混合物以及同时获得乙炔产品的方法，它包括在一系列随后处于低温的阶段中实施预冷却过程。从每个阶段中收集相应各自包括乙炔部分的冷凝物。然后在精馏塔中将这些收集的冷凝物再次混合，以回收乙炔和C2塔顶馏出物部分。然后洗涤塔顶馏出物以去除和回收乙炔。
Pryor等人的美国专利4,002,042号公开了一种用于分离和回收含有氢、甲烷、乙烯、乙烷的原料气中的大(主要)部分。然后。原料气被传送至精馏塔进行分离成为蒸汽流和冷凝流。冷凝流被传送至脱甲烷塔中，在这里被分馏成为塔顶馏出物甲烷-氢流和塔底馏出物乙烯-乙烷流。
Rowles等人的美国专利4,270,940号公开了一种用于从脱甲烷塔顶馏出物中回收乙烷和乙烯的改进的系统。从主回流冷凝器中流出的未冷凝的蒸汽将经受进一步冷凝，并同时在精馏塔中进行精馏。来自精馏塔的液态冷凝物然后被送回脱甲烷塔。
Bauer等人的美国专利4,608,068号公开了方法的改进步骤，适用于从原料流中，如含有氢和C1至C5碳氢化合物的精练厂废气中回收C3+碳氢化合物，包括冷却步骤和至少部分冷凝原料流，以及将部分冷凝的原料流分离成液态部分和气态部分。
Gazzi的美国专利4,657,571号公开了一种用于从高压碳氢气态混合物中回收重组分的多阶段方法。这些步骤包括冷却和部分冷凝碳氢气态混合物，以及从气态混合物获得分离的液体，并送入分馏塔。对未冷凝的气态混合物进行涡轮膨胀。通过所述气态混合物涡轮膨胀后冷凝的液体被分离出来并送入分馏塔。从塔的底部回收重组分。然后，来自第一分馏步骤的气体和来自涡轮膨胀后第二分馏步骤的气体被分别或一起再压缩到被处理气体的运送压力。
Coyle等人的美国专利5,505,049号公开了一种采用具有提高表面的回流热交换器将氮从液化的天然气中去除的方法。将相对温度高的高压液化天然气沿逆流方向引入热交换配置与冷的低压液化的天然气流进行热交换，从而使高压气流变冷，并在回流热交换器中至少部分低压流汽化。如此产生的蒸汽去除了低压流氮。冷的低压流是通过将冷却的高压流进行膨胀获得的。然后将这样膨胀获得的蒸汽与在热交换器中产生的蒸汽混合，然后从热交换器的顶部排出物中将之去除并回收。具有低氮含量的液化的天然气产品是从热交换器底部回收。
尽管许多上述现有技术方法已经在工业上取得了一些成功，但是运转这些系统所消耗的能量是相当高的。因此，在此工业领域需要发展一种方法，本质上具备同样的分馏能力但可降低能量消耗。
发明内容
本发明提供一种改进的分离方法和装置，其实现了优良的分馏并且所需能量降低。
本发明的装置详见附图以及下面的详细描述。该装置包括一个设有多个分馏盘的精馏塔，一个设于精馏塔顶部的回流罐和一个用于塔进料和顶部蒸汽冷却的高架的多制冷剂核心热交换器，以及一个主进料管线，其分为两个进料管线，其中第一个包含较少部分的进料，并进入精馏塔的较低的部分，其中第二个是先通过多制冷剂核心热交换器，然后在第一进料管线上方的一高度处进入精馏塔。
关于该系统的方法操作，采用本发明的装置可获得改良的分馏和分离效果且降低能量需求。起初，将进入本系统的碳氢进料流分为两股料流。进料流的第一部分被送入精馏塔的底部作为汽提蒸汽。进料流的第二部分在核心热交换器中被冷却，然后传送到精馏塔作为塔进料。塔顶部蒸汽在其被引入回流罐前也在核心热交换器中被冷却。从回流罐中涌出的液体靠重力自流被返回到精馏塔作为回流液体。
附图的简要说明
附图是本发明的改进的联合精馏系统的示意图，该系统包括一个精馏塔，一个设于精馏塔顶部的回流罐和一个用于塔进料和塔顶馏出蒸汽冷却的高架的多制冷剂核心热交换器，以及进料系统。
本发明的详细说明
请参见附图，精馏塔2是该精馏系统的基础。精馏塔2设有多个分馏盘4，这是作为相应的期望的分馏步骤所必需的。进入精馏塔的主进料管线6被分为两个进料管线。第一进料管线8包含一小部分的进料，即，进料的大约5％到大约50％，更优选的是大约25％到35％。第二进料管线10包含全部进料的其余主要部分。
进料流的小部分(较少部分)通过管线8进入精馏塔的底部，对该系统起汽提蒸汽(stripping vapor)的作用。
进料流的主要部分通过管线10进入高架核心交换器12，先在其中被冷却，然后再被传送到精馏塔2在高于第一进料管线8的入口上方的一高度处进料。另外，在管线14内的塔顶部蒸汽在进入回流罐16前，也在核心热交换器12中冷却，用于回流。在运转过程中，从塔回流罐排出的液体靠重力自流通过管线18回到精馏塔作为回流液体。从回流罐16的顶部回收的蒸汽通过成品管线20被排出。来自精馏塔2的液体沿管线22被回收用于后续处理。
在本发明的优选实施例中，核心交换器12的冷却方式受到不止一个冷却类型的作用。例如，在附图中，冷却通道24可包括一股或多股乙烯制冷剂流；冷却通道26和28可包括一个膨胀处理蒸汽，冷却通道30可包括氢气制冷剂，冷却通道32可包括甲烷制冷剂。
在回收乙烯的一个实施例中，主进料管线的温度可在-30℃到-85℃范围内。交换器12的冷却剂出口温度比进料气流10的温度要低约1到3℃。离开精馏塔2底部的液体的温度比进料流8的温度要低约3到10℃。
本发明允许使用的装置和方法优于目前公知的用于分馏和分离步骤的系统和装置。用于分馏分离的这些公知的装置中，其中一个被利用和包括在传统精馏系统中。本发明的新颖的热联合精馏系统在能量利用上比公知的传统的系统的效率更高。在典型的传统系统，在核心热交换器中的温度处于接近制冷剂流的返回的温度和精馏塔顶部馏出物温度之间。
相比较，本发明的热联合精馏系统，温度是接近于制冷剂流的返回温度和精馏塔进料温度之间。
按这样的流程，根据本发明系统的运转可以最大限度地利用温度较高的制冷剂，从而减少传统公知精馏系统需要的较低温度的制冷剂的需要量。这个优点可导致实际上的节省制冷用电。
而且，这里所述的热联合精馏系统是在公知的精馏系统基础上的改进。这些装置和方法都能获得和满足相似的精馏要求。然而，这里描述和声明的热联合精馏系统具有更高的能量利用效率，因为它允许在用于工艺的制冷剂流中使用更多有效的更高温度。
另外，一个优点是，即本发明的热联合精馏系统是一个比传统的精馏器更紧凑简洁的设计。传统精馏器的操作原理是基于冷凝的液体膜回流分馏，为了成功的分离效果，需要低速的处理气体。因此，传统精馏器的尺寸就必须比本发明方法的热联合精馏系统大。例如，对使用本发明的热联合精馏系统的一个700KTA乙烯的工厂而言，估计运转所需的场地尺寸是10英尺×20英尺，加上支撑交换器的管道架的面积5英尺×20英尺。对同样的工厂，如果采用如McCue等人的专利4,900,317描述的精馏系统，则所需场地尺寸将更大。本发明装置紧凑简洁设计的优点还包括易于移动和船运，运输，直立，更少有热泄漏的倾向，这是由于与传统精馏器系统相比，冷却单元和精馏塔的表面积减小。
总而言之，与公知的目前使用的用于乙烯或天然气分离工厂分馏轻碳氢化合物的系统相比，本发明的系统提供了一种改进能量效率并降低资金成本并可获得分馏效果的方法。

Claims (13)

1.一种改进的热联合精馏系统，其包括一个具有一系列分馏盘的精馏塔，一个位于所述精馏塔上部的回流罐，和一个与该回流罐相连的高架的多制冷剂核心热交换器，以及一个进料系统，其包括一主进料管线，一进料分流装置，该进料分流装置将该主进料管线分为第一进料管线和第二进料管线，第一进料管线包含较少部分的进料，并引入到精馏塔的较低部分，第二进料管线是先通过所述核心热交换器，然后在第一进料管线上方的一高度处进入精馏塔。
2.如权利要求1所述的改进的热联合精馏系统，其特征在于，该精馏塔具有至少三个分馏盘。
3.如权利要求1所述的改进的热联合精馏系统，其特征在于，该回流罐位于该精馏塔的顶部。
4.如权利要求1所述的改进的热联合精馏系统，其特征在于，该多制冷剂核心热交换器适用于冷却进塔的进料以及提供塔顶馏出蒸汽的冷却。
5.一种改进的热联合精馏处理方法，适用于低分子量碳氢化合物进料混合物的分馏、分离、以及回收，该处理方法包括如下步骤：先将碳氢化合物进料流分成两部分，该进料流中较少的部分被传输进入精馏塔的较低部分，该进料流中较多的部分在核心热交换器里被冷却，然后进入该精馏塔作为进料，其中进料流中较多的部分在比进料流中较少部分进入精馏塔的位置高的位置处进入精馏塔。
6.如权利要求5所述的精馏处理方法，其特征在于，该进料气流中较少的部分是被引入精馏塔的底部，从而对该方法起汽提蒸汽的作用。
7.如权利要求5所述的精馏处理方法，其特征在于，来自所述精馏塔上部的蒸汽流在返回回流系统前都在所述核心热交换器里被冷却。
8.从较重的气态组分分离较轻的气态组分的方法，该方法包括：
(a)将一主进料管线分为第一进料管线和第二进料管线，所述第一进料管线包含较少部分的进料；
(b)将第一进料管线的进料引入精馏塔的较低部分，作为汽提蒸汽；
(c)将第二进料管线的进料在上方的核心热交换器进行冷却；
(d)在高于第一进料管线的位置将第二进料管线的冷却的进料进入该精馏塔，以被精馏；
(e)将顶部馏出蒸汽从该精馏塔移除，使所述顶部馏出蒸汽在该核心热交换器中冷却并部分冷凝，并且从剩余的蒸汽分离部分冷凝的液体；
(f)将部分冷凝的液体返回该精馏塔，作为回流；
(g)回收所述剩余的蒸汽，作为分离出来的较轻的气态组分；以及
(h)从精馏塔底部回收包含较重组分的液体。
9.如权利要求8所述的方法，其特征在于，所述较轻的气态组分包括氢气和甲烷。
10.如权利要求8所述的方法，其特征在于，所述第一进料管线包含的气态进料量比所述第二进料管线的少。
11.如权利要求8所述的方法，其特征在于，所述第一进料管线的进料被引入低于第一分馏盘的该精馏塔的部分。
12.如权利要求8所述的方法，其特征在于，所述核心热交换器在制冷流进口附近有一个较冷的部分，在制冷流的其余位置附近有一个较高温度部分，第二进料管线的进料是在所述上方核心热交换器的该较高温度部分被冷却。
13.如权利要求12所述的方法，其特征在于，所述顶部馏出蒸汽在所述上方核心热交换器的该较冷部分被冷却和部分冷凝。
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