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    • 4. 发明申请
    • A REACTIVE DISTILLATION PROCESS FOR THE ALKYLATION OF AROMATIC HYDROCARBONS
    • 用于芳香烃的烷基化反应的蒸馏过程
    • WO2003076369A1
    • 2003-09-18
    • PCT/US2003/001437
    • 2003-01-16
    • SASOL NORTH AMERICA INC.
    • WINDER, J. BarryWHARRY, Donald L.SCHELL, John R.BROWN, Mary J.MURRAY, Joy L.HOWE, Richard C.SORENSON, Wayne L.SZURA, Daniel P.
    • C07C2/64
    • C07C2/66Y02P20/127
    • A unified process for reactive distillation under pressure for the alkylation of light aromatic hydrocarbons such as benzene and cumene with straight chain C 6 - C 18 olefins using a solid acid alkylation catalyst supported in the reflux zone of the distillation column (column 2). The process is continuous, using a reactive distillation configuration such that at least a portion of the olefin (7) is injected below the benzene rectification zone at the top of the column. The aromatic hydrocarbon (17) is injected continuously at a low rate above the rectification zone (H) at the base of the column and above the reboiler (40). The alkylation reaction takes place primarily in the liquid phase on the solid acid catalyst and is characterized in that the molar ratio is adjustable up to about 100/1, through adjustment of the internal column operating pressure, the benzene reflux rate, the amount of benzene removed from the reflux condenser to storage or from the reboiler with the distillation column operated at or near total aromatic hydrocarbon reflux. The unexpectedly high liquid phase aromatic hydrocarbon to olefin molar ratios achieved in the reactive distillation column increases the selectivity to mono-alkylated aromatics and helps stabilize catalyst lifetime.
    • 使用在蒸馏塔的回流区(柱2)中负载的固体酸烷基化催化剂,在压力下进行反应蒸馏的统一方法,用于烷基化轻质芳烃如苯和枯烯与直链C6-C18烯烃。 该方法是连续的,使用反应蒸馏构型使得至少一部分烯烃(7)被注入塔顶部的苯精馏区下方。 在柱的底部和再沸器(40)上方的芳香族烃(17)以低于精馏区(H)的低速连续注入。 烷基化反应主要发生在固体酸催化剂上的液相中,其特征在于通过调整内部柱的工作压力,苯回流速率,苯的量,摩尔比可调至高达约100/1 从回流冷凝器中取出至储存或从再沸器与蒸馏塔一起运行或接近总芳烃回流。 在反应蒸馏塔中实现的意想不到的高液相芳烃与烯烃摩尔比提高了对单烷基化芳族化合物的选择性,有助于稳定催化剂寿命。
    • 5. 发明申请
    • A REACTIVE DISTILLATION ALKYLATION PROCESS INCLUDING IN SITU CATALYST REGENERATION
    • 包括催化剂再生的反应性蒸馏碱化方法
    • WO2003076074A1
    • 2003-09-18
    • PCT/US2003/001432
    • 2003-01-16
    • SASOL NORTH AMERICA INC.
    • 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
    • B01J38/50
    • B01J29/90B01D3/009C07C2/66Y02P20/127Y02P20/584
    • 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 C 2 -C 30 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 C 4 -C 16 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 C 4 -C 16 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.
    • 将独特的原位催化剂再生过程与压力下的连续反应蒸馏相结合的方法,用于使用在C 2 -C 30烯烃的回流区(21)中负载的固体酸烷基化催化剂烷基化轻质芳烃如C 2 -C 30烯烃 蒸馏塔(A部分)。 催化剂(部分E,F和G)的定期再生通过在塔顶部但在催化剂区上方的苯精馏区下面的C4-C16石蜡(35)逆流注入来进行,而芳族烃 将反应原料(17)连续注入塔的底部的精馏区上方,其中芳族化合物与石蜡分离,副产物从催化剂中洗脱。 使用具有40至90%摩尔分数的芳族化合物的C 4 -C 16石蜡使得能够通过调节柱压力和芳族回流速率来实现和维持约175-250℃的再生温度。 需要显着降低约125至370psig的压力以实现再生温度,而不是仅使用芳烃从催化剂表面稀释和洗涤副产物所需的压力。