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    Continuous process for preparation of dian
    1.
    发明授权
    Continuous process for preparation of dian 失效
    连续的制备过程

    公开(公告)号：US4301305A

    公开(公告)日：1981-11-17

    申请号：US108403

    申请日：1979-12-28

    申请人： Maciej Kiedik ,  Jozef Kolt ,  Jerzy Czyz ,  Edward Grzywa ,  Anna Niezgoda ,  Kazimierz Terelak

    发明人： Maciej Kiedik ,  Jozef Kolt ,  Jerzy Czyz ,  Edward Grzywa ,  Anna Niezgoda ,  Kazimierz Terelak

    IPC分类号： B01J8/00 ,  B01J8/04 ,  C07C37/20 ,  C07C39/12

    CPC分类号： B01J8/006 ,  B01J8/0449 ,  B01J8/0457 ,  C07C37/20 ,  B01J2208/00274

    摘要： The dian is prepared by the condensation of phenol with acetone in the presence of acid ion-exchange catalyst of the type of sulfonated co-polymer of styrene and divinylbenzene. The three-stage process is conducted in two reactors packed with a stationary catalyst bed. In each of the reactors the bed height is 5-20 m and in addition, in both reactors the beds are divided into bottom and upper zones.At various stages of the process, a reaction mixture is circulated with a different linear velocity, the first step of the process being conducted at a temperature of 60.degree.-85.degree. C. in the bed of the first reactor, in succession in the bottom and then upper zone of the catalytic bed; the second stage of the process is accomplished in the bottom zone of the second reactor at a temperature of 70.degree.-90.degree. C.; and the third step is carried out in the upper zone of the second reactor at a temperature of 75.degree.-95.degree. C.The linear velocity of the reaction mixture flow through the bottom zones of the bed is not greater than 10 m/h, and the linear velocity of flow through the upper zones of the reactor bed is not higher than 4 m/h.The sequence of the reaction mixture flow through the reactors is being changed in cycles, and at interstage intervals the reaction mixture is filtered to separate minus mesh and comminuted particles of the catalyst.

    摘要翻译： 在苯乙烯和二乙烯基苯的磺化共聚物类型的酸离子交换催化剂存在下，苯酚与丙酮的缩合制备二胺。 三步法在两个装有固定催化剂床的反应器中进行。 在每个反应器中，床高度为5-20米，此外，在两个反应器中，床分为底部和上部区域。 在该方法的各个阶段，以不同的线速度循环反应混合物，该方法的第一步在第一反应器的床中在60-85℃的温度下连续进行 然后催化床的上部区域; 该方法的第二阶段在第二反应器的底部区域在70-90℃的温度下完成。 第三步骤在第二反应器的上部区域，在75℃-95℃的温度下进行。流经床底部的反应混合物的线速度不大于10m / h， 并且通过反应器床的上部区域的线速度不高于4m / h。 流过反应器的反应混合物的顺序正在循环地改变，并且在间隔间隔过程中将反应混合物过滤以分离催化剂的负网和粉碎颗粒。

    Method for waste recovery from a process of the production of diphenylolpropane
    2.
    发明授权
    Method for waste recovery from a process of the production of diphenylolpropane 失效
    从二羟甲基丙烷生产过程中废物回收的方法

    公开(公告)号：US4131749A

    公开(公告)日：1978-12-26

    申请号：US827780

    申请日：1977-08-25

    申请人： Maciej Kiedik ,  Edward Grzywa ,  Jozef Kolt ,  Kazimierz Terelak ,  Jerzy Czyz ,  Anna Niezgoda

    发明人： Maciej Kiedik ,  Edward Grzywa ,  Jozef Kolt ,  Kazimierz Terelak ,  Jerzy Czyz ,  Anna Niezgoda

    IPC分类号： C07C37/14 ,  C07C37/52 ,  C07C39/06

    CPC分类号： C07C37/52 ,  C07C37/20

    摘要： The essence of the invention consists in heating the dian waste in the presence of sodium hypophosphite as a catalyst in amount of 0.01 - 0.5% by weight at a temperature of 150 to 250.degree. C and under reduced pressure in the range of 5 to 50 mm Hg. As a result a destillate is obtained containing as main components phenol, o- and p-isopropenyl-phenol and their dimers at yield of about 40-74% by weight calculated in relation to the initial amount of dian waste. The distillate obtained was made up with fresh phenol or with phenol and acetone and brought into contact with strongly acid cation exchanger, such as Wofatit KPS, Zerolit 225, Wofatit OK-80, in consequence the o- and p-isopropenylphenol and their dimers reacted with phenol to obtain the dian, the latter being then separated by known methods.

    摘要翻译： 本发明的本质在于在次要亚磷酸钠存在下，在150-250℃的温度和在减压下在5至50mm的范围内以0.01-0.5重量％的量加热二氧化钛 汞。 结果得到含有作为主要组分苯酚，邻 - 和对 - 异丙烯基 - 苯酚及其二聚体的流出物，其产率约为废弃物初始量计算的约40-74重量％。 得到的馏出物用新鲜苯酚或苯酚和丙酮制成，并与强酸阳离子交换剂如Wofatit KPS，Zerolit 225，Wofatit OK-80接触，结果是对 - 异丙烯基苯酚及其二聚体反应 用苯酚获得二胺，然后通过已知方法分离。

    Methods for bisphenol A production
    3.
    发明授权
    Methods for bisphenol A production 失效
    双酚A生产方法

    公开(公告)号：US4906789A

    公开(公告)日：1990-03-06

    申请号：US250393

    申请日：1988-09-28

    申请人： Edward Grzywa ,  Maciej Kiedik ,  Jo Kolt ,  Adam Mazur ,  Jerzy Marszycki ,  Eugeniusz Zajac ,  Anna Rzodeczko ,  Jerzy Czyz ,  Kazimierz Terelak ,  Zbigniew Swiderski ,  Teodor Bek

    发明人： Edward Grzywa ,  Maciej Kiedik ,  Jo Kolt ,  Adam Mazur ,  Jerzy Marszycki ,  Eugeniusz Zajac ,  Anna Rzodeczko ,  Jerzy Czyz ,  Kazimierz Terelak ,  Zbigniew Swiderski ,  Teodor Bek

    IPC分类号： C07C39/16 ,  C07C37/20

    CPC分类号： C07C37/20

    摘要： A process for the production of bisphenol A from phenol and acetone, comprises introducing a substantially anhydrous reaction mixture of phenol, acetone, and recycled solution of bisphenol A and reaction by-products in phenol into a reaction zone containing a cation-exchange resin catalyst, such catalyst being a mixture of resin having a macroporous structure and resin having a microporous structure in a ratio of 0.05:1 to 0.5:1 by weight, the mol ratio of phenol to acetone being 5:1 to 30:1, and the concentration of bisphenol A being 12 to 20% by weight. The temperature of the reaction zone is maintained between 60 degrees and 95 degrees C. The resulting reacted reaction mixture is withdrawn from the reaction zone, the concentration of bisphenol A being 21 to 35% by weight and the amount of reaction by-products being 12 to 24% by weight. Such withdrawn reaction mixture is treated to recover bisphenol A product and to provide the recycled solution of bisphenol A and reaction by-products in phenol.

    摘要翻译： 从苯酚和丙酮生产双酚A的方法包括将苯酚，丙酮和双酚A的再循环溶液和苯酚中的反应副产物的基本上无水的反应混合物引入到含有阳离子交换树脂催化剂的反应区中， 这种催化剂是具有大孔结构的树脂和具有0.05:1至0.5:1重量比的微孔结构的树脂的混合物，苯酚与丙酮的摩尔比为5:1至30:1，浓度 的双酚A为12〜20重量％。 反应区的温度保持在60摄氏度到95摄氏度之间。所得反应的反应混合物从反应区取出，双酚A的浓度为21〜35重量％，反应副产物的量为12 至24重量％。 处理这种取出的反应混合物以回收双酚A产物，并提供双酚A和苯酚中的反应副产物的再循环溶液。