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CN1134748A - 深冷分离 - Google Patents

深冷分离 Download PDF

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CN1134748A
CN1134748A CN94194034A CN94194034A CN1134748A CN 1134748 A CN1134748 A CN 1134748A CN 94194034 A CN94194034 A CN 94194034A CN 94194034 A CN94194034 A CN 94194034A CN 1134748 A CN1134748 A CN 1134748A
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tower
alkene
rich
stream
gas
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E·A·考夫曼
J·A·莫斯
小J·L·皮克林
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ExxonMobil Oil Corp
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Mobil Oil Corp
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
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Abstract

一种分离烃类混合物的方法，该烃类混合物含有一种烯烃、与该烯烃具有相同碳原子数的对应烷烃、以及至少一种较重的烃类组分，其特征在于包括以下步骤：
1)将所述烃类混合物输入至具有上部回流段的第一蒸馏塔(40)；2)从第一蒸馏塔(40)回收富含烯烃和烷烃的第一塔顶馏出气流(40V)，并将该第一塔顶馏出气流传送至第二蒸馏塔(50)的中间蒸馏段；3)从第二蒸馏塔(50)回收富含烯烃的第二塔顶馏出气流(50V)；4)绝热压缩该富含烯烃的第二塔顶馏出气流(50V)，将该压缩的气体传送至第二蒸馏塔(50)的再沸器段(50B)，使该压缩的气体冷却和凝聚，并加热一再沸器液流；
5)闪蒸(64)来自第二蒸馏塔(50)再沸器段(50B)的冷却和凝聚的气体，得到富含烯烃的、部分汽化的闪蒸混合物流；
6)回收并分离该闪蒸混合物流，得到一液体部分(50R)和一气体部分；
7)将所述液体部分(50R)传送至第二蒸馏塔(50)的回流段；
8)从第二蒸馏塔(50)的中段抽出富含烯烃和烷烃的中间液流(40R)，并将所述中间液流(40R)传送至第一蒸馏塔(40)回流段；
9)从第一蒸馏塔(40)回收较重的组分；
10)从第二蒸馏塔再沸器段(50B)回收烷烃；以及
11)回收烯烃产品流。

Description

深冷分离
本发明涉及轻气体的深冷分离，具体地涉及从包含两种或更多轻气体的混合物中回收乙烯或丙烯。
低温技术已被大规模用来回收气态烃类组分，例如各种来源(包括天然气，石油炼制，煤和其它化石燃料)的C1-C2烷烃和烯烃。将高纯度乙烯与裂化烃类排出物流的其它气体组分分离开来，已成为塑料工业化学原料的主要来源。聚合物级乙烯一般含有1％以下的其它材料，可从多种工业过程物流得到。石油炼制中广泛应用烃类的热解和氢化裂解来得到一系列有价值的产物，如裂解汽油、低级烯烃和LPG(液化石油气)，以及副产物甲烷和氢。常规的接近环境温度和压力下的分离技术，可通过依次液化、蒸镏、吸着等回收一系列裂化排出组分。但是，将甲烷和氢与更有价值的C2＋脂族化合物，特别是与乙烯、乙烷、丙烯和/或丙烷分离开来，需要较昂贵的设备和处理能量。我们将把重点放在从裂化气体中回收乙烯的典型大规模低温装置。
典型的低温系统可参看美国专利3,126,267；3,702,541；4,270,940；4,460,396；4,496,380；4,368,061和4,900,347。
本发明的目的之一，是提供一种改进的用以分离轻气体的深冷分离系统，它在能量方面是高效率的，并可节约在低温设备方面的投资。
因此，本发明的一个方面，是一种深冷分离系统，用以分离至少含有三种标准沸点各不相同的挥发性组分的混合物，该系统包括：
1)第一和第二蒸镏塔，每塔各具有上部回流段，中间蒸馏段、和
  下部再沸器段，第二蒸镏塔连接于第一蒸馏塔，接受来自第
  一蒸馏塔的第一塔顶馏出气流；
2)连接于第二蒸馏塔的压缩装置，用以接受来自第二蒸馏塔回
  流段的、富含至少一种低沸点组分的第二塔顶馏出气流，并
  将其绝热压缩；
3)传送装置，用以把来自压缩装置的已绝热压缩的气体传送至
  第二蒸馏塔再沸器段，以使该压缩气体冷凝，并加热再沸器
  液流；
4)闪蒸装置，用以将所述冷凝气体减压，得到富含低沸点组分
  的、部分汽化的闪蒸混合物流；
5)回流流体处理装置，它接受闪蒸混合物流，回收其液体部分
  和气体部分，并将该液体部分传送至第二蒸馏塔回流段；
6)中间液流排送装置，用以从第二蒸馏塔中段排出富含低沸点
  和中沸点组分的中间液流，将其传送至第一蒸馏塔回流段；
7)用以从第一蒸馏塔再沸器段回收至少一种高沸点组分的装
  置；
8)用以从第二蒸馏塔再沸器段回收至少一种中沸点组分的装
  置；以及
9)用以回收低沸点组分的装置。
本发明的另一方面，是一种分离烃类混合物的方法，该烃类混合物含有一种烯烃、与该烯烃具有相同碳原子数的对应烷烃、以及至少一种较重的烃类组分，该方法包括以下步骤：
1)将所述烃类混合物输入至具有上部回流段的第一蒸馏塔；
2)从第一蒸馏塔回收富含烯烃和烷烃的第一塔顶馏出气流，并
  将该第一塔顶馏出气流传送至第二蒸馏塔的中间蒸馏段；
3)从第二蒸馏塔回收富含烯烃的第二塔顶馏出气流；
4)绝热压缩该富含烯烃的第二塔顶馏出气流，将该压缩的气体
  传送至第二蒸馏塔的再沸器段，使该压缩的气体冷却和凝
  聚，并加热一再沸器液流；
5)闪蒸来自第二蒸馏塔再沸器段的冷却和凝聚的气体，得到富
  含烯烃的、部分汽化的闪蒸混合物流；
6)回收并分离该闪蒸混合物流，得到一液体部分的一气体部
  分；
7)将所述液体部分传送至第二蒸馏塔的回流段；
8)从第二蒸馏塔的中段抽出富含烯烃和烷烃的中间液流；
9)将所述中间液流传送至第一蒸馏塔回流段；
10)从第一蒸馏塔回收较重的组分；
11)从第二蒸馏塔再沸器段回收烷烃；以及
12)回收烯烃产品流。
本发明可主要用于分离含有大量乙烯、乙烷和/或丙烯/丙烷的C2－C4＋气体混合物。裂化烃类气体中通常伴有相当多数量的氢和甲烷，以及少量C3＋烃类、氮、二氧化碳和乙炔。乙炔组分可在低温操作之前去除。典型的石油炼制尾气或石蜡裂化排出气一般可经过预处理，去除任何酸性气体，并在吸水的分子筛上干燥至露点为145°K，以制得低温原料混合物。典型的原料气体为含10—50摩尔％乙烯、5—20％乙烷、10—40％甲烷、10—40％氢、以及最高达10％C3烃类的裂化气体。该原料是脱甲烷的，也可脱丙烷和/或脱乙烷，以浓聚适用于本改进方法的料流中的所需组分。
在一较佳实施例中，室温或更低温度下、工作压力为2500千帕〔350磅/平方英寸(表压)〕以上，最好为约3700千帕〔520磅/平方英寸(表压)〕的干燥压缩裂化原料气体在低温条件下的冷冻组合中，分离为几股液流和甲烷/氢气流。较有价值的乙烯的回收纯度很高，适用于常规聚合反应。
以下将参照附图更具体说明本发明，其中：
图1是说明利用裂化和冷冻分馏来制备乙烯的典型烃类处理装置各单元操作安排的流程示意图；
图2是一详细的过程和设备图，详细说明了多级蒸馏塔部分，该部分是用以将低温馏分脱丙烷，并将一C3流分裂为丙烯和其它产品流。
参看图1，图中所示的处理装置包括常规的烃类裂化单元10，它将新鲜的烃类原料12以及可随意加入的再循环烃类13转变为裂化烃排出料流。裂化单元排出物在分离单元15用常规技术分离为液态产物15L、C3—C4石油气15P、和一种裂化的轻气流15G，这轻气流中主要包含甲烷、乙烯、和乙烷，并带有不同数量的氢、乙炔和C3＋组份。裂化的轻气用压缩机16加压至工作压力，并通过热交换装置17、18冷却至环境温度以下，得到作为以下所述的深冷分离过程的原料。
冷却的加压气体原料流在多个顺序设置的分馏器型精馏单元20，24中进行分离。每个精馏单元的连接方式是使其运行时冷凝的液体从上部的精馏器热交换器部分20R、24R通过重力流动而聚集在其下部的圆筒部分20D、24D，热交换器包括许多垂直地设置的间接热交换通道，来自下部圆筒部分的气体向上通过这些通道，在其中与温度更低的制冷剂流体或其它冷冻介质进行间接热交换而被冷却。向上流动的富含甲烷的气体部分地冷凝在热交换通道的垂直表面上，形成回流的液体，直接与向上的气流接触，得到更冷的向下流动的凝聚液流，从而逐渐使凝聚液流中富集乙烯和乙烷组分。
较好的系统设有将干燥原料气体引入初级精馏区或冷冻组的装置，初级精馏区或冷冻组包括多个串接的，依顺序逐步更冷的精馏单元，它们将原料气体分离为在低温回收的初级富含甲烷气流20V以及至少一种初级凝聚液流22，该液流富含C2烃类组分，也含有少量甲烷。
使至少一种初级凝聚液流从初级精馏区通入具有串接的脱甲烷器区30、34的分馏系统，去除甲烷而使之净化。在热交换器31中采用中度低温来冷冻来自第一脱甲烷分馏区30的塔顶馏出物，以便从第一脱甲烷器塔顶馏出气流32中回收初级凝聚液流中的大部分甲烷，同时回收基本不含甲烷而富含乙烷和乙烯的第一脱甲烷底部液流30L。最好第一脱甲烷器塔顶馏出气流是用中度低温制冷剂(例如可从丙烯制冷环路获得的制冷剂)冷却，以提供回流液体30R，再循环至第一脱甲烷区30的顶部。
将第一脱甲烷器塔顶馏出气流中的至少一部分在超低温的末级脱甲烷区34进一步分离，可得到一种富含乙烯的料流，这时回收得到液态的第一富含乙烯的烃类粗产物流34L以及末级脱甲烷器超低温塔顶馏出气流34V。使末级脱甲烷器塔顶馏出气流34V通过超低温热交换器36，进入末级精馏单元38，得到末级超低温液体回流38R，再循环到末级脱甲烷分馏器的顶部，就可回收所有残余的乙烯。这时回收得到基本不含C2＋烃类的、富含甲烷的末级精馏塔顶馏出气流38V。利用这种双重脱甲烷技术，总的脱甲烷热交换负荷，主要由热交换单元31中的中度低温制冷剂承担，而将C2＋烃类与甲烷和较轻组分分离开来所需的制冷总能量得以减少。将第一脱甲烷区的C2＋底部液流30L在脱乙烷分馏塔40中进一步分馏，可得到乙烯产物所需的纯度，这时在C3＋流40L去除C3和更重的烃类，并提供第二粗乙烯流40V，按照改进了的操作技术，这种乙烯流是作为没有显著冷凝或直接回流的气体回收的。
本发明通过把塔顶馏出气流40V通入一中间蒸馏塔单元50(普通称为C2产品分离器)，可提高运行的经济效率，并降低主要的设备要求。从蒸馏塔50通过塔顶馏出物50V回收富含乙烯的气体。另外，将第二粗乙烯流40V和第一富含乙烯的烃类粗产物流34L进行共分馏，以得到纯化的乙烯产物，从而获得聚合物级的产物。底部乙烷流50L可随意地再循环至裂化单元10，通过在热交换器17、18和/或20R中与中度冷冻的原料进行间接热交换而回收其热值。C3＋流40L可送至后继的分馏设备以回收丙烯、丁烯等有价值的组分。
塔顶馏出气流50V在压缩机单元60被绝热压缩，以便以加到再沸器50B的热泵的形式回收能量。其后气流50V可任选地来自补充冷却器(trim cooler)62的支流合并，在闪蒸装置64减压，部分地冷凝该富含乙烯气流。将该部分冷凝气流输入分相器的容器66，由此回收液体回流50R(把它输入至蒸馏塔50的回流段)，以及未冷凝的气流69(它与塔顶馏出气流50V合并以便再压缩)。乙烯产物可方便地以液流68形式从压缩器60回收。
从蒸馏塔50靠近气流40V的入口处，抽出C2液流40R，将该液流40R通入分馏塔40上段作为回流，可以实现本发明的主要优点。有效回流比保持低于0.5，较好为1∶5至1∶10，最好为约0.15(回流液体的重量/塔顶馏出气流总重量)。本发明的这一特点可从本发明的运行与现有蒸馏技术的比较看出。
C2低温回收系统的一个主要优点，是可在相同的蒸馏塔中以较低的压力，获得较高效率的乙烷、乙烯分离。将相邻的两个塔的“脐带式”(umbilical)回流装置合并起来，可进一步节约本技术的设备成本。
图2显示了一种改进的丙烯回收分馏系统，其中的顺序编号与图1中的相当设备对应。原料例如为富含丙烯的原料流130L，这种原料经过脱乙烷，去除了C2一组分和重裂化液体，得到含有丙烯、丙烷和C4＋组分(如丁烯和丁烷)的气体或液体原料。可以使用多个液体或气体原料流，例如附加原料流130A。如图2所示，系统中有第一和第二蒸馏塔140、150，每塔各自有上部回流段，中间蒸馏段，和下部再沸器段，其连接方法是使第二蒸馏塔150在中段接受来自第一蒸馏塔140的第一塔顶馏出气流140V。系统中包括用以将第二蒸馏塔的工作压力控制在预定压力的常规装置，例如在典型低温流体处理系统中的压缩机、泵、和阀门等控制装置。
一般单级压缩就已足够，但在图2所示的例子中，使用了多级压缩装置160A、160B，它们连接于并接受来自第二蒸馏塔上部回流段的富含至少一种低沸点组分(如丙烯)的第二塔顶馏出气流150V，将之绝热压缩。用导管装置161将绝热压缩后的气体从末级压缩器160B通至第二蒸馏塔的再沸段150B以冷凝该压缩气体并加热液体再沸器料流。
系统中装有闪蒸装置，以便将凝聚气体减压，得到富含低沸点组分的部分汽化的闪蒸混合物流。可以用单个闪蒸单元达到这一目的，但最好通过一系列膨胀涡轮机164A，164B来降压，它们在流体流动方向是连通的，在机械方面则连接到相对应的压缩机，以便在减压步骤中回收闪蒸膨胀的能量。中间分离单元165提供中间气流165V，与第一级压缩气流160C混合起来，作为输入至第二级压缩机160B的原料。
分离单元166设有回流流体处理装置，它接受闪蒸混合物流164V，回收的液体部分150R通至第二蒸馏塔150的回流段。泵压装置140P用导管连接起来，用以将富含低沸点和中沸点组分(如丙烯和丙烷)的中间液流140R从第二蒸馏塔150的中段抽出，送至第一蒸馏塔140的回流段。所需的回流比(即低于0.5的回流比)可用常规的流体处理装置(如泵140P，阀门装置，比例控制器等)控制。
在底部导管140L回收来自第一蒸馏塔再沸器段的至少一种高沸点组分(如C4＋)，在导管150L回收来自第二蒸馏塔再沸器段的至少一种中沸点组分(如再烷)；而在导管168回收来自压缩机160B的低混点组分(如丙烯)。
为了从这种“脐带式”结构获得充分的利益(这种结构中初级蒸馏单元的回流热负载是由第二蒸馏单元的精馏提供)，最好提供常规的流体控制装置，使第一蒸馏单元的工作压力维持在不显著地高于第二蒸馏单元工作压力的数值，通常不比第二绝对压力10—20％以上。在将丙烯与更重的烃类分离时，脱丙烷塔在较低压力下工作，就可在其再沸器段中以较低温度运行，从而避免在这区域中产生不希望发生的反应，尤其是不饱和C4烃类(如丁烯和二烯)的聚合。
实施例
以下给出按照本发明制备聚合物级乙烯的物料平衡和能量要求，并与常规低温蒸馏方法比较。在下列的表中，所有单元都是基于稳态连续流条件，每股物流中各组分的相对数量都是以100份重量的料流为基准的。也给出了脱乙烯器和C2分裂塔运行的条件。
            每100公斤流率(Stream rate)中的物流组分
                    (公斤/100公斤)物流号(图1)        30L         40V         40R          40L           50L          68          50R乙烯         66.61       71.61       59.49        0.00          0.08        99.89        99.89乙烷         23.57       28.19       40.48        0.25         99.04         0.11         0.11丙二烯        0.80        0.00        0.00        8.35          0.00         0.00         0.00丙烯          7.36        0.20        0.03       74.24          0.87         0.00         0.00丙烷          1.66        0.00        0.00       17.16          0.01         0.00         0.00
    100.00公斤  100.00公斤  100.00公斤  100.00公斤    100.00公斤   100.00公斤    100.00公斤
                                      每100公斤流率中的焓
                                          (千焦/100公斤)30L          40V          40R         40L          50L          68           50R-7,098       +23,241      -17,138     +3,620       -11,735      +30,135      -20,378脱乙烷塔塔顶压力(千帕)                                859.75塔顶温度(°K)                                  222.7底部温度(°K)                                  289.8回流比(公斤回流/公斤塔顶馏出气)                 0.15C2分裂塔塔顶压力(千帕)                                790.80塔顶温度(°K)                                  214.4底部温度(°K)                                  235.6回流比(公斤回流/公斤塔顶馏出气)                 0.70每100公斤系统进料的工作负荷(千焦/100公斤)脱乙烷再沸器                                  34,766脱乙烷冷凝器(略)                                  无C2分裂塔再沸器                               48,142C2分裂塔补充冷却器                           35,504C2分裂塔热泵                                 25,443
熟悉低温工程的技术人员会理解，各单元的运行配置，与常规的回流型蒸馏单元相比，可降低对回流的冷却要求。
这种低压、脱乙烷器/C2分裂器结合起来的系统，与常规的高压、脱乙烷器/C2分裂器分开的系统相比，过程致冷要求低20％。此外，脱乙烷器/C2分裂器结合起来的系统的主要设备成本也比常规系统低。低压脱乙烷器/C2分裂器结合的优点可体现在两个方面：低压脱乙烷的优点，和利用C2分裂塔来回流脱乙烷器的优点。
脱乙烷塔在较低的塔顶压力工作(859.75千帕，常规压力为2983.33千帕)，可便于乙烷与丙烯的分离。分馏性能的提高，是因为乙烷对丙烯的相对挥发性，与蒸馏压力之间成反比关系。性能的提高，表现为在上述低压脱乙烷塔中，对回流的要求较低。在乙烯回收单元中，低压脱乙烷塔的工作回流比保持在0.2以下，最好为0.15，而在常规高压脱乙烷塔中，要求的回流比为0.38。
低压脱乙烷塔中回流要求降低，带来了两个直接的好处：(1)减少了将脱乙烷塔塔顶馏出气凝聚所需的过程致冷量。因为要求的回流少，需要凝聚的气体就少。结果节约了致冷系统压缩机的操作费用；(2)由于回流体积较小，也降低了回流泵压费用。
低压脱乙烷塔的另一个好处是可以用正在冷凝的丙烯致冷剂来再沸该塔。低压脱乙烷塔所需的再沸器温度低于高压脱乙烷塔(289.8°K与344.4°K相比)。低压脱乙烷塔中较低的再沸器温度近似等于高压丙烯致冷剂的冷凝温度(露点温度)。因此，低压脱乙烷塔再沸器可用来冷凝致冷剂，从而为致冷系统提供能量节约。
利用从C2分裂塔抽出的液体来提供脱乙烷塔的回流，这样的设计其成本比常规脱乙烷塔/C2分裂塔分开的系统低。两种塔结合或分开的系统都要求相同的蒸馏塔，塔再沸器，和C2分裂塔热泵设备。但是常规的脱乙烷塔/C2分裂塔系统需要脱乙烷塔塔顶冷凝器和脱乙烷塔回流筒，而在本发明的两种塔结合起来的系统中却不需要这些设备。结果两种塔结合的系统的总设备成本比常规系统低。
从C2分裂塔抽出的液体对C2分裂塔的运行并无显著影响。C2分裂塔中的液流率要比抽出供脱乙烷塔回流用的液体数量高一个数量级。当脱乙烷塔的回流是由C2分裂塔抽出时，C2分裂塔热泵的功率要求只增大了不到3％。
省去脱乙烷塔冷凝器，就足以补偿C2分裂塔补充冷却器负荷的增加而有余。在脱乙烷塔/C2分裂塔系统中需要致冷的是脱乙烯塔冷凝器和C2分裂塔补充冷却器这两个单元。在低压脱乙烷塔/C2分裂塔结合的系统中，总致冷要求可比常规系统净降低20％。

Claims (9)

1.一种深冷分离系统，用以分离至少含有三种标准沸点各不相同的挥发性组分的混合物，其特征在于它包括：
1)第一和第二蒸馏塔，每塔各具有上部回流段、中间蒸馏段、和下部再沸器段，第二蒸馏塔连接于第一蒸馏塔，接受来自第一蒸馏塔的第一塔顶馏出气流；
2)连接于第二蒸馏塔的压缩装置，用以接受来自第二蒸馏塔回流段的、富含至少一种低沸点组分的第二塔顶馏出气流，并将其绝热压缩；
3)传送装置，用以把来自压缩装置的已绝热压缩的气体传送至第二蒸馏塔再沸器段，以使该压缩气体冷凝，并加热再沸器液流；
4)闪蒸装置，用以将所述冷凝气体减压，得到富含低沸点组分的、部分汽化的闪蒸混合物流；
5)回流流体处理装置，它接受闪蒸混合物流，回收其液体部分和气体部分，并将该液体部分传送至第二蒸馏塔回流段；
6)中间液流排送装置，用以从第二蒸馏塔中段排出富含低沸点和中沸点组分的中间液流，将其传送至第一蒸馏塔回流段；
7)用以从第一蒸馏塔再沸器段回收至少一种高沸点组分的装置；
8)用以从第二蒸馏塔再沸器段回收至少一种中沸点组分的装置；以及
9)用以回收低沸点组分的装置。
2.如权利要求1所述的分离系统，其特征在于它还包括压力控制装置，用以将第一蒸馏塔的工作压力保持在高于第二蒸馏塔的工作压力，但不比第二蒸馏塔的工作压力大20％以上。
3.一种分离烃类混合物的方法，该烃类混合物含有一种烯烃、与该烯烃具有相同碳原子数的对应烷烃、以及至少一种较重的烃类组分，其特征在于该方法包括以下步骤：
1)将所述烃类混合物输入至具有上部回流段的第一蒸馏塔；
2)从第一蒸馏塔回收富含烯烃和烷烃的第一塔顶馏出气流，并将该第一塔顶馏出气流传送至第二蒸馏塔的中间蒸馏段；
3)从第二蒸馏塔回收富含烯烃的第二塔顶馏出气流；
4)绝热压缩该富含烯烃的第二塔顶馏出气流，将该压缩的气体传送至第二蒸馏塔的再沸器段，使该压缩的气体冷却和凝聚，并加热一再沸器液流；
5)闪蒸来自第二蒸馏塔再沸器段的冷却和凝聚的气体，得到富含烯烃的、部分汽化的闪蒸混合物流；
6)回收并分离该闪蒸混合物流，得到一液体部分和一气体部分；
7)将所述液体部分传送至第二蒸馏塔的回流段；
8)从第二蒸馏塔的中段抽出富含烯烃和烷烃的中间液流；
9)将所述中间液流传送至第一蒸馏塔回流段；
10)从第一蒸馏塔回收较重的组分；
11)从第二蒸馏塔再沸器段回收烷烃；以及
12)回收烯烃产品流。
4.如权利要求3所述的方法，其特征在于步骤(9)是在有效回流比不大于0.50的条件下实施的。
5.如权利要求3或4所述的方法，其特征在于步骤(9)是在有效回流比不大于0.15的条件下实施的。
6.如权利要求3—5所述的任一方法，其特征在于步骤(7)是在有效回流比不大于0.50的条件下实施的。
7.如权利要求3—6所述的任一方法，其特征在于它还包括将第一蒸馏塔的绝对压力保持在比第二蒸馏塔的绝对压力大10％以内的步骤。
8.如权利要求3—7所述的任一方法，其特征还在于所述的烯烃为乙烯，而所述的烷烃为乙烷。
9.如权利要求3—7所述的任一方法，其特征还在于所述的烯烃为丙烯，而所述的烷烃为丙烷。
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