具有中间再沸器和中间冷凝器的二元精馏塔操作线斜率分析和理论板数计算  

Derivation of the Slopes of Operating Line and Calculation of Theoretical Plates for the Binary Distillation Column with Intermediate Reboiler and Intermediate Condenser

作　　者：邓春 陆炫彤 Deng Chun;Lu Xuantong(China University of Petroleum,Beijing 102249,China)

机构地区：[1]中国石油大学化学工程与环境学院重质油国家重点实验室,北京102249

出　　处：《山东化工》2020年第7期245-250,共6页Shandong Chemical Industry

基　　金：北京高校“优质本科课程”《化工原理》;中国石油大学(北京)教改项目:“《化工原理》混合式教学课程建设”,“化工原理核心课程建设”和“《化工系统工程》教学内容的革新”。

摘　　要：对于设置中间再沸器和中间冷凝器的二元精馏塔,本文首先提出将精馏塔划分为精馏段、中间冷凝段、精馏中间段、提馏中间段、中间再沸段和提馏段,对各段的操作线的斜率进行严格推导和分析,并利用逐板计算法计算理论板数。以苯-甲苯二元精馏分离的实例进行分析,计算出各段的操作线方程。案例分析结果表明,设置中间换热的精馏塔理论板数比常规精馏塔的理论板数多10.23块,并在y-x图中绘制McCabe-Thiele图,直观显示设置中间换热器精馏塔的理论板数增加。This paper firstly divide the binary distillation column with intermediate reboiler and intermediate condenser into rectifying section,intermediate condensing section,intermediate rectifying section,intermediate stripping section,intermediate reboiling section and stripping section.The slope of each operating lines is strictly derived and analyzed.The number of theoretical plates is calculated by the plate-by-plate calculation method.An example of binary distillation separation of benzene-toluene is analyzed,and the operation line equations of each segments are calculated.The results show that the theoretical number of the distillation column with the intermediate reboiler and intermediate condenser is 10.23 plates more than that of the conventional rectification column.The McCabe-Thiele diagram is drawn on the y-x equilibrium diagram,which visually shows that the number of theoretical plates of the distillation column with the inter-exchanger is increased.

关 键 词：中间再沸器 中间冷凝器 精馏塔操作线 McCabe-Thiele图 逐板计算法 

分 类 号：TQ053.5[化学工程]