万吨粗苯精制工艺设计.docVIP

毕 业 设 计 题目：8万吨/年粗苯精制工艺设计 系 别：化学与化学工程系 专 业：化学工程与工艺 姓 名： 学 号： 指导教师： 设计说明 此设计的任务是处理量为8万吨/年的粗苯精制工艺设计，它采用了粗苯低温加氢工艺流程，选用了连续精馏筛板塔的化工设备。 原料粗苯经过两苯塔实现轻重组分分离，其中塔釜重质苯做为产品回收，塔顶轻苯在加氢反应器中进行加氢反应后进入脱轻塔脱除硫化氢，氨气等低沸物，然后依次进入预精馏塔 萃取精馏塔 纯苯塔和二甲苯塔，最终得到纯净合格苯、甲苯的产品。 为达到设计要求，此设计通过物料衡算、热量衡算、塔的工艺尺寸计算、塔板负荷性能验算及附属设备计算，得到符合要求的一系列工艺流程参数，包括进料量F=106.055Kmol/h,塔顶液体流量D=90.945Kmol/h,塔底釜液流量W=15.11Kmol/h，塔径D=1.6m,塔高h=24.45m,板间距，精馏段实际塔板数，提馏段塔板数，设置7个人孔，出塔顶塔底人孔外其他人孔处的板间距为H=0.7m,进料处板间距H=1m等。 根据这一系列工艺流程参数绘制工艺流程图、物料衡算图及主设备图。 关键词：低温加氢精制、连续精馏筛板塔、两苯塔、苯、甲苯  Design elucidation This design task is productivity for eight million tons/year cuben refining process design, it adopted cuben cryogenic hydrogenation process, choose the continuous distillation tower chemical equipment sieve. Raw material cuben after two benzene tower, which achieve weight component separation tower kettle heavy benzene as product recycling, tower light benzene in hydrogenation reactor in hydrogenation reaction took off after removal from the light tower into hydrogen ammonia and other low boiling, which in turn into that gets distillation column of pure benzene tower and extract xylene tower, and ultimately the pure qualified benzene, toluene products. To achieve the design requirements, this design through the material calculation, heat calculation, tower craft size calculation, tower plate load performance checking and affiliated equipments calculation, get to meet the requirements of a series of process parameters, including into 106.055 Kmol feed F = liquid flow, being/h D = 90.945 Kmol/h, bottom kettle fluid flow W = 15.11 Kmol/h, tower diameter D = 1.6 m, high tower 24.45 m, board h = distance, rectifying section number and mention actual tower plate, plate number distillated section tower set seven people hole, a tower in the bottom and the other manhole manhole for h = 0.7 board spacing, feeding place board m distance h = 1-m etc. According to this series of process parameters rendering process flow diagram, mat