化工原理课程设计题目：甲苯冷却器的设计姓名张风平学号201007120153年级2010级专业化学工程与工艺系（院）化学化工学院指导教师张杰2013年6月设计任务（一）设计题目甲苯冷却器的设计（二）计任务及操作条件1)甲苯入口温度95℃，出口温度45℃2)冷却介质循环水，入口温度20℃，出口温度自定；3)允许压降不大于50KPa；4)每年实际生产时间：7000小时/年，处理量：95000吨/年；（三）设备类型管壳式换热器（四）厂址临沂地区（五）设计内容1）设计方案简介：对确定的工艺流程及换热器的型式进行简单论述。2）换热器的工艺计算和主要结构尺寸设计。3）管程和壳程压力降的核算。4）设计结果概要或设计结果一览表。5）对本设计的评述及有关问题讨论。2目录1、设计概述····························52、确定设计方案··························62.1选择换热器的类型·······················62.1.1工作原理··························62.1.2换热管布置和排列间距····················62.1.3换热器设计的基本原则····················72.1.4流体流速的选择·······················73、确定物性数据··························73.1定性温度··························84、估算传热面积··························84.1热流量····························84.2平均传热温差·························84.2.1计算平均温度差·······················84.2.2计算R和P·························84.3传热面积···························94.4冷却水量···························95、工艺结构尺寸··························105.1管径和管内流速························105.2管程数和传热管数·······················105.3计算换热器的实际换热面积和总传质···············105.4壳体内径···························105.5折流板····························115.6折流板数···························1136.换热器核算···························116.1热流量核算··························116.1.1管内表面传热系数···························116.1.2污垢热阻和管壁热阻························126.1.3计算传热系数KC··························126.1.4该换热器的面积裕度···························126.2换热器内流体的流动阻力···························136.2.1管程流体阻力···························136.2.2壳程阻力···························137、设计评述·····························148、主要符号说明···························1519、参考文献····························1541.设计概述热量传递的概念与意义1.1热量传递的概念热量传递是指由于温度差引起的能量转移，简称传热。由热力学第二定律可知，在自然界中凡是有温差存在时，热就必然从高温处传递到低温处，因此传热是自然界和工程技术领域中极普遍的一种传递现象。1.2化学工业与热传递的关系化学工业与传热的关系密切。这是因为化工生产中的很多过程和单元操作，多...
