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    A REACTIVE DISTILLATION ALKYLATION PROCESS INCLUDING IN SITU CATALYST REGENERATION
    2.
    发明公开
    A REACTIVE DISTILLATION ALKYLATION PROCESS INCLUDING IN SITU CATALYST REGENERATION 有权
    包括原位催化剂再生的活性蒸馏烷基化工艺

    公开(公告)号：EP1480746A1

    公开(公告)日：2004-12-01

    申请号：EP03703858.5

    申请日：2003-01-16

    申请人： Sasol North America Inc.

    发明人： WINDER, Barry, J. ,  WHARRY, Donald, L. ,  SCHELL, John, R. ,  BROWN, Mary, J. ,  MURRAY, Joy, L. ,  HOWE, Richard, C. ,  SORENSON, Wayne, L. ,  SZURA, Daniel, P. ,  GATES, Frank

    IPC分类号： B01J38/50 ,  B01J38/38 ,  B01J38/56 ,  C07C5/22

    CPC分类号： B01J29/90 ,  B01D3/009 ,  C07C2/66 ,  Y02P20/127 ,  Y02P20/584

    摘要： A unified process which couples a unique in-situ catalyst regeneration process with a continuous reactive distillation under pressure for the alkylation of light aromatic hydrocarbons such as benzene with C2-C30 olefins using a solid acid alkylation catalyst supported in the reflux zone (21) of a distillation column (section A). Periodic regeneration of the catalyst (sections E, F and G) is carried out with a countercurrent injection of a C4-C16 paraffin (35) below the benzene rectification zone at the top of the column, but above the catalyst zone while the aromatic hydrocarbon reaction feedstock (17) is injected continuously at a point above a rectification zone at the base of the column where the aromatic compound is separated from the paraffin and by-products washed from the catalyst. The use of the C4-C16 paraffin with the aromatic at a mole fraction in the range of 40 to 90% enables a regeneration temperature of about 175 - 250°C. to be achieved and maintained by adjusting the column pressure and aromatic reflux rate. Significantly lower pressures, on the order of 125 to 370 psig, are required to achieve regeneration temperature than would be otherwise required with the use only of the aromatic hydrocarbon to dilute and wash the by-products from the catalyst surfaces.

    摘要翻译： 将独特的原位催化剂再生方法与压力下的连续反应性蒸馏相结合的统一方法，用于使用固体酸烷基化催化剂将苯与C2-C30烯烃进行烷基化，所述固体酸烷基化催化剂负载于 蒸馏塔（部分A）。 催化剂的周期性再生（部分E，F和G）是在塔顶部的苯精馏区以下逆流注入C4-C16链烷烃（35），但在催化剂区上方进行的，而芳烃 将反应原料（17）连续地注入塔底部的精馏区之上的一个点，其中从链烷烃中分离出芳族化合物和从催化剂中洗出副产物。 具有在40-90％范围内的摩尔分数的芳族C 4 -C 16链烷烃的使用能够实现约175-250℃的再生温度。 通过调整色谱柱压力和芳香族回流率来实现和维持。 需要显着较低的压力，大约125至370psig的压力以实现再生温度，这比仅使用芳烃稀释并清洗催化剂表面副产物所需的温度要高。