化工设计答辩终稿

二硫化碳-四氯化碳蒸馏分离过程与精馏塔的设计湖南师范大学“大闹化工队”团队成员：郭骏、王瑛璞、韩鹏指导老师：赵海红设计任务书1)生产能力：10吨每小时（料液）2)原料组成：34%的二硫化碳和66%的四氯化碳（摩尔分率，下同）3)产品组成：馏出液97%的二硫化碳，釜液5%的二硫化碳4)操作压力：塔顶压强为常压5)进料温度：58℃6)进料状况：自定7)加热方式：间接蒸汽加热8)塔板效率:0.5；9)建厂地址：湖南长沙地区；10)其他参数（除给出外）可自选。目录摘要······················································3前言······················································4第一章设计方案简介·································61.1流程的设计及说明·······························61.2已知参数···········································71.3选塔依据··········································7第二章设计计算······································92.1精馏流程的确定··································92.2塔的物料衡算····································102.3塔板数计算········································11第三章板式塔主要工艺尺寸设计计算············163.1塔工艺条件及物性数据计算···················163.2精馏塔气液负荷计算····························203.3塔和塔板主要工艺尺寸计算···················203.4筛板的流体力学验算····························253.5塔板负荷性能图··································29

3.6精馏塔的计算结果总表·························36第四章精馏塔的附属设备以及接管尺寸·········394.1接管设计···········································394.2塔总高度计算

·····································404.3热量衡算············································414.4再沸器的选择······································444.5泵的选型············································444.6主要符号说明······································46参考文献·················································49设计结果评述与小结··································50致谢·······················································51附录·······················································53人员分配BOSS:赵海红老师“艺术总监”：韩鹏“项目经理”：郭骏“高级工程师”：王瑛璞原料液经过预热器预热后进入精馏塔内。操作时连续的从再沸器中取出部分液体作为塔底产品（釜残液）。再沸器中原料液部分汽化，产生上升蒸汽，依次通过各层塔板。塔顶蒸汽进入冷凝器中全部冷凝，然后进入回流罐，并将冷凝液送回塔顶作为回流液体，其余部分经过冷凝器后被送出作为塔顶产品。为了使精馏塔连续的稳定的进行，流程中还要考虑设置原料槽、产品槽和相应的泵。为了便于了解操作中的情况及时发现问题和采取相应的措施，常在流程中的适当位置设置必要的仪表，比如流量计、温度计和压力表等，以测量物流的各项参数。

设计方案的选定物料衡算能量衡算塔的位置CS2的质量分率平均分子量（g/mol）物料衡算kmol/h塔顶aD=0.941MD=78.34D=24.73进料aF=0.203MF=127.48F=53.71塔釜aW=0.0251MW=150.1W=78.44单位总热量Qv塔顶溜出液热量QD回流热量QR进料热量QF塔底残液热量QW水蒸气还需要提供热量Qh冷凝器消耗的热量Qc再沸器提供的热量QBkJ/h3526022918353277186372925444999279331064693450568物料流程图塔板数的确定确定方法根据相平衡方程和操作线方程，采用逐板计算求得塔板数理论板数总理论板数为11（包括蒸馏釜），精馏段理论板数为5，第6板为为进料板，提馏段理论板数为6∴NT=（11-1）=10层（不包括塔釜）

塔板效率

ET=0.5

实际板数精馏段：N精=5/ET=5/0.5=10层；提馏段：N提=5/ET=5/0.5=10层计算表格xD=0.9700y1=0.9700x1==0.9258y2=0.9354x2=0.8482y3=0.8478x3=0.7296y4=0.7822x4=0.5810y5=0.6661x5=0.4351y6=0.5522x6=0.3225xf=0.3330y7=0.4568x7=0.2451y8=0.3412x8=0.1666y9=0.2241x9=0.1003y10=0.1251x10=0.0523y11=0.0535x11=0.0214xw=0.05塔体工艺尺寸的确定板间距的选择板间距取0.4m

塔径的确定将提馏段与精馏段取相同的塔径，故取1.4m塔板主要工艺尺寸的确定

塔板类型筛板塔

板上液体的流型单流型

是否分块是分四块塔板结构（区域、开孔数目）取边缘区宽度Wc=0.035m，安定区宽度Ws=0.065m

塔板结构图主体设备装配图塔板的流体力学验算类型雾沫夹带量eV筛板的稳定性系数k液泛m单板压降pa精馏段提馏段塔板负荷性能图操作弹性操作弹性

pp配管计算管型进料管回流管塔底出料管塔顶蒸汽出料管塔底蒸汽进气管规格接管尺寸由内蒸汽速度及体积、流量决定，各接管允许的蒸汽速度查表得标准设备的选型选型方法再沸器的选择选择120℃水蒸气加热，传热系数取出料液温度

泵的选型由额定流量和扬程确定公称直径1mm管程数NP排管数n管程流通面积1m2换热面积A/m2换热管长度L/mm40041290.005955.64500型号50AY-60B流量10扬程m40功率机4轴2.9转速2950效率37%泵壳许用压力16126结构单级

致谢经过两个多月的化工原理课程设计，我已明白课程设计对我来说的意义，它不仅仅是让我们把所学的理论知识与实践相结合起来，提高自己的实际动手能力和独立思考的能力，更重要的是同学间的团结，虽然我们这次花去的时间比别人多，但我相信我们得到的也会更多!

作为一名化工学院的大三学生，我觉得课程设计是十分有意义的，而且是十分必要的。在已度过的大学时间里，我们在课堂上掌握的仅仅是理论知识，如何