CN1220178A - 改进的分凝分馏塔系统 - Google Patents

改进的分凝分馏塔系统 Download PDF

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CN1220178A
CN1220178A CN97111162A CN97111162A CN1220178A CN 1220178 A CN1220178 A CN 1220178A CN 97111162 A CN97111162 A CN 97111162A CN 97111162 A CN97111162 A CN 97111162A CN 1220178 A CN1220178 A CN 1220178A
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fractionating column
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CN1070385C (zh
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王松汉
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China Petrochemical Corp
Sinopec Beijing Petrochemical Engineering Co
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Sinopec Beijing Petrochemical Engineering Co
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Abstract

改进的用于分离气体混合物的分凝分馏塔系统,包括分凝分馏器、塔段和塔釜,所述分凝分馏器设在塔的上部,其特征在于分凝分馏器为板翅式分凝分馏器。

Description

改进的分凝分馏塔系统
本发明涉及一种改进的分离设备及其应用，更具体地说，涉及用于分离气体混合物的分凝分馏塔系统及其在分离裂解气中的应用。
气体混合物的分离包括传热和传质过程，故而强化传热和传质对改进气体混合物的分离效果至关重要。例如，在石油化工中，为了从裂解气中分离出符合要求的乙烯和丙烯产品，经常采用低温深冷分离方法，即采用串联的激冷换热器系统，通过外加冷剂，在低温深冷条件下使气体混合物冷却或冷凝而部分液化，初步分离为气相和液相，进而再经过精馏等一系列操作过程将气体混合物分离，得到高纯度的产品。这种方法需要消耗大量低温冷量和耐低温合金材料。有鉴于此，近十年来，人们对深冷分离工艺及其设备进行了许多改进，以提高冷量利用效率，节省低温设备投资。其中一个重要的改进就是采用分凝分馏器来进行气体混合物的冷凝，并已用至塔系统中，构成分凝分馏塔系统，以强化传热和传质。例如，美国专利U.S.P4,657,571中描述的分馏塔17包括分凝分馏器38，日本专利特开平5-87447、6-337192和6-341760中也公开了包括分凝分馏器的精馏塔，这些专利说明书中对分凝分馏器的形式均未作具体说明，但附图中所示的均为列管式。这种形式的分凝分馏器因表面积有限，传质、传热效果不是特别理想，且在实用时不易控制回流，特别是操作负荷不能太大，否则易发生液泛。故如何改进分凝分馏塔的传热和传质，提高塔的分离效率，对于提高塔的处理能力、降低成本有重要意义。
本发明人对于分凝分馏塔的构成和运行规律作了深入研究，发现分凝分馏塔的分离效率主要取决于分凝分馏器的传热、传质性能，为此，本发明人对各种形式的分凝分馏器用于分凝分馏塔系统进行了尝试，发现板翅式分凝分馏器与塔段结合使用可获得极好的分离效果，基于此即完成了本发明。
因此，本发明的目的是提供一种改进的分凝分馏塔系统，它包括板翅式分凝分馏器、塔段和塔底。
本发明的另一个目的是提供所述改进的分凝分馏塔系统在分离气体混合物中的应用。
图1为本发明的分凝分馏塔的构成示意图；
图2为本发明图1的分凝分馏塔的另一种构成示意图，其中还设有再沸器；
图3为本发明的分凝分馏塔的另一种构成示意图，其中设有多个板翅式换热器和塔段；
图4为本发明图3的分凝分馏塔的另一种构成示意图，其中还设有再沸器；
图5为现有技术的分凝分馏塔的构成示意图；
图6为本发明图1的分凝分馏塔用于裂解气分离的流程组合图；和
图7为常规的裂解气分离流程图。
下面结合附图对本发明作详细说明。
在本发明中，所谓“分凝分馏器”是指将气体混合物冷却而使高沸点馏分冷凝的设备，其中包括适用于此目的的各种换热设备。
在本发明中，气体混合物也包括蒸汽混合物。
如图1所示，本发明的分凝分馏塔系统包括板翅式分凝分馏器1、塔段3和塔釜4，其中板翅式分凝分馏器1置于塔的上部，塔段3位于塔的中部，板翅式分凝分馏器1和塔段3之间有液体分配器2。
在本发明中，板翅式分凝分馏器使用板翅式换热器。板翅式换热器为已知设备，关于其构成等可参见中国大百科全书总编辑委员会《化工》编辑委员会，《中国大百科全书·化工》第9页第一栏第23-38行(中国大百科全书出版社，1987第1版)(引入该内容作为参考，并构成本说明书的一部分)。在本发明中，优选板翅式换热器的换热面积至少为800m2/m3，更优选至少1000m2/m3。板翅式换热器可设置供多股冷剂出入、流通的通道，这样，就可同时通入多股冷剂物流。
在本发明的分凝分馏塔中，塔段可为常见的结构形式，例如为塔板式、浮阀式、泡罩式和填料式等中的至少一种，但优选为填料塔段。填料材质、形式不受特别限制，只要不与所分离的气体混合物发生化学作用即可。
在本发明的分凝分馏塔系统中，底部设塔釜4。
如图2所示，在本发明的分凝分馏塔系统的一种实施方案中，可以设有再沸器5。
如图3所示，在本发明的另一种结构形式中，设有两套分凝分馏器和塔段，即整个塔系统的构成从上到下为分凝分馏器1、塔段3、分凝分馏器1’、塔段3’和塔釜4。当然，塔系统内也可以设有多套分凝分馏器和塔段，这些都在本发明范围之内。如图4所示，在这种结构形式的塔系统中，也可以设再沸器5。
本发明的分凝分馏塔系统一般从塔段进料，冷剂通入板翅式换热器内。气体混合物在该换热器内上升时，部分重组分冷凝，形成冷凝液沿翅片呈膜状向下流动，并与上升气体混合物逆向接触，气、液之间既传热、又传质，故而分离效率高。从板翅式换热器内流出的冷凝液体经液体分配器进入塔段，在塔段内与上升气体发生传热、传质作用，进一步强化分离效果。经分离后，气体物流从塔顶出口引出，而液相物流从塔釜出口流出。
本发明的分凝分馏塔系统可用于各种气体混合物的分离，例如它们可串联连接，并任选结合其它分离设备，组合成分离流程。图6为本发明的分凝分馏塔用于裂解气分离的流程示意图。裂解气304经过换热器冷却和冷凝，然后经过三个分凝分馏塔，三个分凝分馏塔的底部液体分别作为第一和第二脱甲烷塔的进料(也可将两个或多个分凝分馏塔的底部液体作为第一和第二脱甲烷塔的进料)。第一分凝分馏塔压力为3.0-3.5MPa，顶部温度为-25～-40℃，底部温度为-15～-25℃；第二分凝分馏塔压力为3.0-3.4MPa，顶部温度为-50～-85℃，底部温度为-30～-50℃；第三分凝分馏塔压力为2.8-3.3MPa，顶部温度为-100～-140℃，底部温度为-60～-90℃。由于分凝分馏塔分出的气量大，改善了脱甲烷塔的操作条件，冷机功率可比常规方法节省10％以上。
用下列实施例进一步说明本发明。
                    实施例1
采用如图1所示的改进的分凝分馏塔对气体混合物进行分离作业。其中板翅式换热器的换热面积为900m2/m3。填料为散装填料IMTP，不设再沸器。
以下列组成(重量百分比)的物流作为进料305，按147390kg/小时的量送入本发明的塔系统：
      H2    CH4    C2     C3  C4     合计
      1.3    19.0    50.0    19.4  0.4    100进料温度为-20℃，进料点为塔的中部。结果如下：
塔顶气体306：
    总量     74194kg/小时
    温度       -37℃
组成：
      H2    CH4    C2   C3   C4     合计
      2.7    33.4    59.5   4.4   0.0    100
塔底液体307：
    总量     731961kg/小时
    温度       -20℃
组成：
      H2    CH4   C2     C3     C4     合计
      0.1    5.2    42.0    34.5    18.2    100
                    比较例1
进料305组成与实施例1相同，按147390kg/小时进料，进料温度亦为-20℃。但塔系统为现有技术的塔系统，如图5所示，它与实施例中所用的塔结构相似，只是分凝分馏器采用换热面积为300m2/m3的列管式换热器，塔段为塔板式塔段。结果如下：
塔顶气体306：
    总量    57098kg/小时
    温度    -37℃
组成：
      H2   CH4   C2   C3   C4     合计
      3.3   38.9   52.7   5.0   0.1    100
塔底液体307：
    总量    90292kg/小时
    温度    -37℃
组成：
      H2    CH4   C2     C3     C4     合计
      0.1    7.4    50.0    28.6    13.9    100
由所得结果可知，在进料一样的情况下，现有技术的塔分离出的气体为57098kg/小时，而本发明的分凝分馏塔为74194kg/小时，多约30％。同时，分凝分馏塔分出的液相中重组份也多，塔所需的冷量也比现有技术的塔少10％以上。
                    实施例2
本实施例说明本发明的分凝分馏塔用于裂解气分离的应用。
如图6所示，压力为3.48MPa，温度为-12℃的裂解气，经过换热器冷却和冷凝，然后经过三个分凝分馏塔，第一分凝分馏塔压力为3.0-3.5MPa，顶部温度为-25～-40℃，底部温度为-15～-25℃。第二分凝分馏塔压力为3.0-3.4MPa，顶部温度为-50～-85℃，底部温度为-30～-50℃。第三分凝分馏塔压力为2.8-3.3MPa，顶部温度为-100～-140，底部温度为-60～-90℃。三个分凝分馏塔的底部液体分别作为第一和第二脱甲烷塔的进料。第一脱甲烷塔压力为0.5MPa到3.5MPa，第二脱甲烷塔压力为0.6MPa。表1列出分凝分馏塔流程的裂解气组成(304点)和其它点311、312、314、315的数据，从表1可知分离出的H2、CH4约为2083kg-mol/小时。
                               表1
                 分凝分馏塔流程主要数据点的温度、
                 压力、流量及主要成份的百分组成
     物流号     304      311       312      314      315
相态     进料混相  第一脱甲烷塔塔底液相  第三分凝分馏塔塔顶汽相  第二脱甲烷塔塔顶汽相  第二脱甲烷塔塔底液相
                                   百分组成：
      氢气    15.16      0      43.38     7.25       0
      甲烷    28.00      0.01      56.16     92.38      0.01
      乙烯    34.00      49.04      0.30     0.29      92.74
      乙烷    7.77      16.01       0      0      6.74
      丙烯    10.92      25.40       0      0       0
       C4    4.15      9.54       0      0       0
     总流率kg-mol/小时    6263.0      2670.17      2082.74     631.44      877.70
     温度℃   -12.8     -8.41     -114.67     -134.78     -65.40
     压力kg/cm2    34.85      20.24      32.22      6.08      6.11
                   对比例2
采用类似于图6的图7流程，并在相似条件下操作，只是分凝分馏塔改为分离罐。结果如表2所示。
                               表2
                  常规分离流程主要数据点的温度、
                 压力、流量及主要成份的百分组成
    物流号     304     311         312      314      315
相态     进料混相 第一脱甲烷塔塔底液相      第三分离罐塔顶汽相  第二脱甲烷塔塔顶汽相  第二脱甲烷塔塔底液相
                                 百分组成：
    氢气    15.16       0       81.5        4.9       0
    甲烷    28.00      0.01       18.2        94.7       0
    乙烯    34.00      55.5       0.30        0.30      91.5
    乙烷    7.77      14.6        0        0      7.8
    丙烯    10.92      22.4        0        0      0.7
    C4    4.15      7.5        0        0       0
   总流率kg-mol/小时    6263.0      3054       1069        1645      495
   温度℃    -12.8      -8.41       -114.67        -134.78     -65.40
    压力kg/cm2    34.85      20.24       32.22        6.08      6.11
由表2可知，常规分离流程分出的H2、CH4只有1069kg-mol/小时，仅为分凝分馏塔流程分出气量的一半。故而分凝分馏塔改善了脱甲烷塔的操作条件，而且使冷机功率节省10％以上。

Claims (10)

1．改进的用于分离气体混合物的分凝分馏塔系统，包括分凝分馏器、塔段和塔釜，所述分凝分馏器设在塔的上部，其特征在于分凝分馏器为板翅式分凝分馏器。
2．按权利要求1的分凝分馏塔系统，其特征在于还包括再沸器。
3．按权利要求1的分凝分馏塔系统，其特征在于板翅式分凝分馏器的换热面积至少为800m2/m3。
4．按权利要求3的分凝分馏塔系统，其特征在于板翅式分凝分馏器的换热面积至少为1000m2/m3。
5．按权利要求1的分凝分馏塔系统，其特征在于板翅式分凝分馏器设有供多股冷剂出入、流通的通道。
6．按权利要求1的分凝分馏塔系统，其特征在于塔段为筛板塔、浮阀塔、泡罩塔和填料塔的至少一种。
7．按权利要求6的分凝分馏塔系统，其特征在于塔段为填料塔。
8．权利要求1的分凝分馏塔系统在分离气体混合物中的应用。
9．按权利要求8的应用，其特征在于气体混合物为裂解气。
10．采用包括权利要求1的分凝分馏塔系统在内的分离设备分离的气体产品。
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