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    • 4. 发明公开
      KR1020080077104A 비스페놀-Ａ 플랜트 수율 향상 방법 无效
    • 비스페놀-Ａ 플랜트 수율 향상 방법
    • 双酚A植物提高
    • KR1020080077104A
    • 2008-08-21
    • KR1020087010866
    • 2006-08-24
    • 바져 라이센싱 엘엘씨
    • 에비트스티븐디 , 페츠코스테판더블유 , 치청-밍
    • C07B61/00 , C07C37/20 , C07C37/08 , C07C39/16
    • C07C45/53 , C07C2/66 , C07C37/20 , C07C37/72 , C07C37/74 , C07C37/84 , C07C407/00 , C07C409/10 , Y02P20/127 , C07C15/085 , C07C49/08 , C07C39/16
    • An improved process is provided for producing bisphenol-A (BPA) comprising steps of (1) contacting benzene and a C3 alkylating agent, e.g. propylene, isopropanol or propyl chloride, under alkylation conditions with an alkylation catalyst in a reaction zone to produce an alkylation effluent comprising cumene; (2) oxidizing the cumene from step (1) to produce the corresponding hydroperoxide; (3) cleaving the hydroperoxide from step (2), to produce product comprising phenol and acetone; (4) reacting acetone with a stoichiometric excess of phenol under acidic conditions, possibly in the presence of a cocatalyst or promoter, e.g. a thiol compound, to form a reaction product stream comprising crude bisphenol-A product, unreacted phenol, possibly unreacted acetone, possibly cocatalyst or promoter, water of condensation, and other reaction byproducts; (5) distilling in single or multistage the reaction product stream from step (4) to distill off a volatilized unreacted phenol stream, possibly an unreacted acetone stream, possibly a stream containing cocatalyst or promoter if present in step (4), and the water of condensation, while sending downstream to a BPA-phenol adduct crystallization and purification step, said purification step comprising one or more solid-liquid separation and wash steps, the resulting concentrated BPA phenolic feed stream consisting essentially of phenol in which the bisphenol-A and byproducts have been concentrated; (6) producing BPA-phenol adduct crystals by crystallization of the concentrated BPA phenolic feed stream in said crystallization, solid-liquid separation and wash steps with cooling for said crystallization by vaporization of an alkane hydrocarbon or mixture of hydrocarbons containing from 4 to 6 carbons, e.g. pentane; (7) separating the BPA-phenol adduct crystals by solid-liquid separation, such as, for example, by centrifugation or filtration, and washing same in one or multiple stages with a wash phenol stream which may include at least a portion of the volatilized unreacted phenol stream recovered from step (5), or spent wash or mother liquor from subsequent crystallization, solid-liquid separation, and wash steps, to produce final washed BPA-phenol adduct, final spent wash and final mother liquor; (8) cracking a stream comprising at least a portion, for example from about 0.5 to about 20 wt.%, preferably from about 1 to about 10 wt.%, more preferably from about 2 to about 7 wt.%, of said final mother liquor of step (7) in a reactor with basic or acidic cracking catalyst, for example caustic or aluminum chloride, under cracking conditions selected to recover a product comprising from about 60 to about 90 wt.% of said portion of said mother liquor stream as phenol having a purity level of from about 95 to about 100 wt.%, and from about 10 to about 40 wt.% of said cracked stream as heavy residue byproduct; and (9) recovering and feeding the phenol product of step (8) to step (4) and/or step (7).
    • 提供了用于生产双酚-A（BPA）的改进方法，包括以下步骤：（1）使苯和C3烷基化剂接触，例如， 丙烯，异丙醇或丙基氯，在烷基化条件下与反应区中的烷基化催化剂反应生成包含枯烯的烷基化流出物; （2）从步骤（1）氧化枯烯以产生相应的氢过氧化物; （3）从步骤（2）中切割氢过氧化物，以产生包含苯酚和丙酮的产物; （4）在酸性条件下，可能在助催化剂或助催化剂存在下，使丙酮与化学计量过量的苯酚反应。 形成包含粗双酚-A产物，未反应的苯酚，可能未反应的丙酮，可能的助催化剂或助催化剂，缩合的水和其它反应副产物的反应产物流; （5）单步或多步地蒸馏步骤（4）的反应产物流，以蒸发掉挥发的未反应苯酚物流，可能未反应的丙酮物流，可能含有助催化剂或助催化剂的物流（如果存在于步骤（4）），并且水 的冷凝，同时向下游送入BPA-苯酚加合物结晶和纯化步骤，所述纯化步骤包括一个或多个固液分离和洗涤步骤，所得浓缩的BPA酚类进料流基本上由酚组成，其中双酚A和 副产品已经集中; （6）在所述结晶，固液分离和洗涤步骤中通过在浓缩的BPA酚进料流中结晶来生产BPA-苯酚加合物晶体，冷却所述结晶，通过蒸发含有4至6个碳原子的烃或烃的混合物 ，例如 戊烷; （7）通过固液分离（例如通过离心或过滤）分离BPA-苯酚加合物晶体，并用洗涤苯酚流在一个或多个阶段洗涤，其可以包括至少一部分挥发的 从步骤（5）回收的未反应的苯酚流，或用于后续结晶，固液分离和洗涤步骤的废洗涤液或母液，以产生最终洗涤的BPA-苯酚加合物，最终洗涤和最终母液; （8）裂化含有至少一部分的物流，例如约0.5至约20重量％，优选约1至约10重量％，更优选约2至约7重量％的所述最终 在具有碱性或酸性裂化催化剂，例如苛性碱或氯化铝的反应器中的步骤（7）的母液在选择的回收产物的条件下回收包含所述母液流的所述部分的约60至约90重量％ 作为具有约95至约100重量％的纯度水平的苯酚和约10至约40重量％的作为重残余副产物的所述裂化物流; 和（9）将步骤（8）的苯酚产物回收和进料至步骤（4）和/或步骤（7）。
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