甲苯冷却器的设计 (2).doc

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1、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

2、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。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···················

3、·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·····

4、······················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···············

5、············116.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

6、.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····························151.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

7、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，多需要进行加热和冷却，例如：化学反应通常要在一定的温度进行，为了达到并保持一定温度，就需要向反应器输入或输出热量；又如在蒸发、蒸馏、干燥等单元操作中，都要向这些设备输入或输出热量。此外，化工设备的保温，生产过程中热能的合理利用以及废热的回收利用等都涉及到传热的问题，由此可见；传热过程普遍的存在于化工生产中，且具有极其重要的作用。总之，