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以2-甲基萘气固相催化氧化制备2-甲基-1,4-萘醌体系为研究对象,设计了三塔连续减压精馏工艺,并利用Aspen Plus软件对整个分离过程进行了模拟计算。通过选择物性方法和组分的简化、DSTWU模块的简捷设计和Rad Frac模块的严格计算,应用模型分析工具优化得到了粗酚系统连续减压精馏的工艺参数。若各塔轻关键组分的回收率设为98%,在一定的进料条件下,塔1、塔2、塔3的理论塔板数分别为10、13和19;最佳进料位置分别在6、9和10块板;塔顶产品与进料的质量流中之比(D/F)分别为0.293 3、0.191 2和0.647 6。得到2-甲基萘、2-甲基-1,4-萘醌和苯酐产品的质量分数分别为99.9%、99.0%和99.9%。该过程得到的结果对开发更为高效便捷的粗酚分离精制方法具有一定参考价值。
The 2-methyl-1,4-naphthoquinone system was prepared by solid phase catalytic oxidation of 2-methylnaphthalene. The three-column continuous vacuum distillation process was designed and the whole separation process was carried out by using Aspen Plus software Simulation calculation. Through the selection of physical methods and components simplification, the simple design of DSTWU module and the rigorous calculation of Rad Frac module, the process parameters of continuous vacuum distillation of crude phenol system were optimized by using the model analysis tools. If the recovery rate of key components of light tower is set at 98%, the theoretical plate numbers of tower 1, tower 2 and tower 3 are 10, 13 and 19, respectively under a certain feeding condition. The optimal feeding locations are respectively At plates 6, 9 and 10; the mass flow-to-feed ratio (D / F) of overhead products to feed was 0.293 3, 0.1991 and 0.647 6, respectively. The mass fractions of 2-methylnaphthalene, 2-methyl-1,4-naphthoquinone and phthalic anhydride were 99.9%, 99.0% and 99.9%, respectively. The results of this process have some reference value for the development of more efficient and convenient crude phenol separation and purification methods.