直径1800mm的甲苯筛板精馏塔设计（全套CAD图+说明书+开题报告+翻译）
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毕业设计（论文）任务书学 院： 机 械 工 程 学 院 题 目： 直径1800mm的甲苯筛板精馏塔设计 起止时间： 学生姓名：专业班级：指导老师：教研室主任院 长：设计（论文）内容及要求：一、 已知设计参数： 生产能力8万吨/年（300天） 进料组成50%（质量） 塔顶产品组成 99% 塔底产品组成 2% 操作压力：常压 进料热状态： 泡点进料 冷却水： 加热蒸汽： 塔类型：板式塔 环境：衡阳室外二、 设计内容及设计工作量要求： （1）按所给设计参数完成分离塔的施工图设计; （2）绘制设计图纸总计3张零号以上，其中要求手工绘图1张壹号以上； （3）设计说明书字数不少于1.5万字，并要求统一用A4纸打印； （4）翻译3千左右汉字量的与毕业设计有关的英文资料； （5）撰写相当于3百汉字的英文摘要。三、 主要参考资料:化工设备设计全书（塔设备）化工原理化工工艺设计手册GB150-1998钢制压力容器 指导老师： 指导教师： 年 月 日 毕业设计(论文)题 目 直径1800mm的甲苯筛板精馏塔设计学院名称 机械工程学院 指导教师职 称班 级学 号学生姓名 毕业设计（论文）开题报告设计（论文）题目直径1800mm的甲苯筛板精馏塔设计设计（论文）题目来源自选设计（论文）题目类型工程设计起止时间一、 设计（论文）依据及研究意义：本设计依据化工工艺设计手册、GB150-1998钢制压力容器、JB/T4710-2005钢制塔式容器以及HG20562-1998塔设计技术规定进行。本设计的作用在于分离化工生产中常用到的两种重要化工原料苯和甲苯，意义重大。综合考虑分离效率、生产制造成本、安装及维护等因素，本设计采用筛板式精馏塔。二、 设计（论文）主要研究的内容、预期目标（技术方案、路线）：本设计主要从化工工艺、材料选型、结构设计以及塔的机械设计进行设计。本设计路线：分离任务工艺流程描绘工艺计算材料选型结构设计塔的机械设计附属设备选型。预期目标：希望通过本次的毕业设计能培养出独立设计的能力，为以后的工作打下好的基础，更好的与社会接轨。三、设计（论文）的研究重点及难点：重点是：依据分离任务进行分离工艺的计算确定塔体和塔板的工艺尺寸，由塔的操作条件完成塔体和裙座的厚度计算，由塔的安装环境对塔进行机械校核。难点：一、由于资料可能不全，设计时没有经验，造成各种误差。二、分离效率的保证三、塔的结构设计四、设计（论文）研究方法及步骤（进度安排）：1月6日至2月15日：了解我们所要设计的试验装置，为进行设计做准备； 2月16日至2月28日：进行参观实习；写开题报告； 2月28日至3月18日：查阅资料，找设计依据，理出设计思路； 3月18日至4月24日：具体的结构和系统设计，求得设计的各种依据； 4月25日至5月25日：设计，画出设计图纸； 5月26日至5月28日；整理图纸，进行打印；排版设计说明书。 5月29日至5月31日：准备答辩。五、进行设计（论文）所需条件： 1、要有充分的资料（与塔设备有关、与分离工艺有关）。 2、到相关单位进行实习，了解塔设备的结构及生产过程中的各种控制方案和原理。 3、设计所需设计方法、软件、工具等。六、指导教师意见： 签名： 年 月 日摘要：在化工、炼油、医药、食品及环境保护等工业部门，塔设备是一种重要的单元操作设备。塔器即是高径比很大的设备。它可以实现气（汽）-液相或液-液相之间的充分接触，从而达到相际间进行传质及传热的目的。常见的、可在塔设备中完成的单元操作有：精馏、吸收、解吸和萃取等。精馏是分离液体混合物最常用的一种单元操作，即利用液相混合物中各相分挥发度的不同，使易挥发组分由液相向气相转移，难挥发组分由气相向液相转移。苯和甲苯都是化工生产中的重要原料，属于芳香族化合物。因此，将苯和甲苯从其混合物中分离出来加以提纯，意义重大。塔设备按结构形式可分为填料塔和板式塔。由于板式塔的分离效果比填料塔好，考虑到苯和甲苯的物性以及生产费用问题，本设计选用化工生产中被广泛采用的筛板塔。因为筛板塔较其他类型塔有如下优点：结构简单，成本低，塔板效率高，安装维修方便。本设计的主要内容是：过程的物料衡算、热量衡算，工艺计算，结构设计和校核，机械强度设计(特别是要考虑风载荷和地震载荷的影响)，管路选择，贮罐、换热器的选型，绘制工艺流程图，以及塔的施工图设计：包括总装配图和若干零件图。关键词： 精馏 筛板塔 工艺计算 结构设计 强度校核 Abstract: The tower equipment is an important unit operation equipment in industry sectors, for instance, chemical industry, refinery, medicine, food, environmental protection, and so on. It can realize the steam between the liquid phase or the fluid - liquid phase contact deeply, thus achieving the border carries on the mass transfer and the heat transfer goal. The distillation is the separation of liquid mixtures most commonly used as an unit operation in chemical industry, oil refining, petrochemical and other industries. The design mission is to produce an important chemical raw material from a mixture of benzene and toluene, it will be a great significance if the material can be separated from its mixture of benzene and toluene. Taking into account the structures of benzene and toluene, as well as the production costs, the designer selected the sieve plate distillation column which are widely used in chemical production.As compared to other types of towers, the sieve-plate column tower has the following advantages: simple structure, low cost, high efficiency tray, tower installation and maintenance easy. The main elements of the design is: Process material balance, heat balance, process calculation, structural design and verification, mechanical strength of the design, pipe selection, storage tank, heat exchanger, drawing process maps, design of tower construction plans, including the total number of assembly drawings and parts diagram.Key Words: Distillation Sieve-plate column Process calculation Structural design Check of strength目录第一章 概述1第二章 流程的设计及说明3第三章 工艺设计计算4 3.1 物料衡算4 3.2 确定塔内操作温度5 3.3 确定回流比及塔板数6 3.4 塔设计计算8 3.4.1 精馏段计算8 3.4.2 提馏段计算 20 3.5 精馏塔高度的计算33第四章 精馏塔的结构设计34 4.1 塔盘34 4.2 各接管及法兰选择35 4.3 人孔40 4.4 操作平台和扶梯41 4.5 裙座42 4.6 吊柱43第五章 塔体和裙座的机械设计45 5.1 选择材料和确定参数45 5.2 计算筒体和封头的厚度465.3 塔的自振周期的计算465.4 塔体的质量载荷计算475.5 风载荷及风弯矩计算505.6 地震载荷及弯矩的计算525.7 各载荷引起的轴向应力545.8 筒体和裙座危险截面的强度与稳定性校核565.9 筒体和裙座水压试验应力校核575.10 裙座和塔体的连接焊缝校核595.11 基础环设计605.12 地脚螺栓计算61 第六章 附属设备的计算及选型 65 6.1 贮罐65 6.2 换热器66参考文献69英文翻译70 谢辞85iv 英文翻译Chinese Jof ChemEng，9(2)141144(2001)Operation of a Batch Stripping Distillation Columnxu Songlin(许松林) ，Jose Espinosab，Hector ESalomoneb and Oscar AIribarrenba National Engineering Research Center for Distillation Technology，Tianjin University,Tianjin 300072，Chinab Institute for Development and Design INGAR ,Conicet，Santa Fe，ArgentinaAbstract A stripping batch distillation column is preferred when the amount of the light component in the feed is small and the products are to be recovered at high purityThe operation modes of a batch stripping are believed to be the same as those of a rectifier Howeverthe control system of a stripper is different In this paper，we explore three different control methods with Hysys(Hyprotech Ltd1997)for a batch stripperThe main difference is the control scheme for reboiler liquid level：(a)controlled by reflux flow；(b)controlled by reboiler heat duty；(c)controlled by bottom product flow The main characteristics of operating a batch stripper with different control scheme are presented in this paperGuidelines axe provided for the startup of a batch stripper，the effects of some control tuning parameters on the column performance are discussedKey words batch strippercontrolOperation1 INTRODUCTONBatch process is becoming more popular as chemical process industries move toward manufacturing fine and specialty chemicals，where flexibility is a key issue due to the frequent change of product demandBatch distillation columns are inherently flexible，as a single column call separate many different components from a multicomponent feedThus the use of batch distillation is becoming more important for the seperation and purification of highvalue chemicalsin many chemical ,food，and pharmaceutical industriesTraditionally the most popular kind of batch distillation column is the so-caled rectilying columnwhich has a large reboiler，to which al the feed is chargedan different products are removed from the top There are three ways to operate a rectifying column2They are：(1)constant reflux and variable distillate composition，(2)variable reflux an d constant distillate composition of key component，(3)optimal reflux policy which trades of(1)and(2)and is based on the most profitable operation Batch stripping column is opposed to a batch rectifier It has its storage vessel at the top and the products leave the column at the bottom A stripping batch distilation column is preferred when the amount of the light component in the feed is small and the products are to be recovered at high purity4,5 The operation modes of a batch stripping are believed to be the same as those of a rectifier Howeverthe control system of a stripper is differentIn this paper，we explore three different control methods with Hysys(Hyprotech Ltd1997)for a batch stripperThe control schemes are shown in Fig1 The main difference is the control scheme for reboiler liquid level：(a)controlled by reflux flow，(b)controlled by reboiler heat duty，(c)controled by bottom product flow The main characterics of operating a batch stripper with different control scheme are presented in this paperGuidlines are provided for the startup and the effect of so e control turning parameters on the column performance are discussed.2 EXPERIMENTAL APPARTUS FOR THE SIMULATIONSThe experimental apparatus in the simulations is the same for the three control schemesThe stripping column has a reboiler，a condenser and 15 traysThe volumes of the reboiler and the condenser are 2m3 and 5m3，respectivelyThe diameter of the column is 0.5 mThe feed is the mixture of methanol(0.05)and ethanol (095)(mole fraction)The liquid percent level set point for the reboiler is 50 and the mixture takes 80 of the whole volume of the condenserAt the beginning，the trays are dry startup，but the reboiler is charged with the same mixture to the liquid level set pointThe specification of bottom product ethanol is 0999All the simulated experimental procedures are that the stripper is started up till the specification of the heavy key composition is reached，then the bottom product valve is opened so that the product leavesthe column，the product valve is shut down when the product composition declines to the specification3 RESULTS AND DISCUSSION31 Control reboiler Hquid level by reflux flow In this control scheme【Fig1(a)】，the reboiler liquid percent level is controlled autom atically by reflux flow，the reboiler heat input and bottom product flow are controled manualy At the beginning，the reboiler heat in put is set fixedThe reboiler liquid level declines as the light com ponent is vaporizedWhich will cause reflux flow down the reboiler automaticallyThe control of the reboiler liquid level is reversibleSo when the reboiler liquid level is higher，there wil be less reflux flow an d vice versa. When the composition of heavy key component gets to its specification，the bottom product flow valve is opened；once it declines to the specification，the bottom product flow valve is shut down manualyIn this case，when ethan ol corn -position reaches 0999，the bottom product flow valve is opened ，when ethan l is less than 0999 the bottom product flow valve is shut down The dynamic process of this operation mode is shown in Fig2There is a time lag between the reboiler liquid level an d reflux flow ，especially when the number of stages is largeIn order to get a stable reboiler liquid level control during the whole operation，two aspects should be considered carefully0ne is to use an appropriate reflux valve If the reflux valve is oversized，the reboiler liquid level controller wil get more reflux flow to the reboiler than the set point when the liquid level declines Then the reflux flow valve will be closed This makes the reboiler liquid level fluctuate frequentlyOne case is shown in Fig3In this situation the heavy key component composition in the bottom is unstable The other aspect is that the tuning parameter of the reboiler liquid level should be chosen appropriately when a proportional only bottom level controler is employedThe proportional gain of the controler should be between 40and 80If is too small，it is difficult to get a stable reboiler liquid level contro1Fig4 shows the relation between reboiler liquid percent level and for the same reboiler dutyFrom Fig4it is obvious that if is less than 40 the liqui d percent level in the reboiler is far away from the set point level 50If is between 40 and 80，the liquid level in the reboiler is near the set point32 Control reboiler liquid level by reboiler heat inputIn this control scheme Fig1(b)】，the reboiler liquid level is controlled by reboiler duty automatically,reflux and bottom products flow are controlled manuallyAt the beginning，the reflux flow valve is opened to a fixed valueReboiler liquid level increases，which will cause heat input to the reboilerThe action of the reboiler liquid level controler is direct，which means that the higher the reboiler liquid level，the more the heat input to the reboiler and vice versaWhen the com position of the heavy key component in the reboiler gets to its specificationthe bottom product flow valve is opened manuly When the heavy key component com position decreases to 0999，the valves for bottom product an d reflux flow are shut down manuallyFig5 shows the dynamic process of this operation mode It is obvious that the boil up mass flow and the liquid levels of condenser and reboiler are fluxed at the startup of the operationThis is due to the dynamic responsiveness of reboiler heat input to the liquid level controller33 Control reboiler Hquid level by bottom product flowThe reboiler liquid level is controled by bottom product flow in this control schemeFig1(c)】This scheme is similar to the third control mode for a rectifierin which the reboil ratio is variable In order to get the bottom product specification，a total reboil process should be established at the beginning of the operationThe action of the reboiler liquid level controller is direct，which means that the higher the liquid level，the more the bottom product flow and vice versaFigure 6(b)shows that at the startup of this operation，the liquid levels in both reboiler and condenser are oscillated，since it is difficult to meet the requirement for the total reboil at the beginning of the operation，for the reflux flow and reboiler heat input are operated manually4 CONCLUSIONThe dynamic simulation with Hysys for the operation of a batch stripping distillation column indicates the main characterics of this kind of column，in which three different control schemes are employedIn the first scheme，reboil ratio is constant with variable bottom product com position；in the second scheme，reboil ratio is variable and the heavy key component composition in the bottom product is nearly constant，and the third is an optim al operation which could obtain more profit Among these three control modes，the third is the most difficult to operate，since both controllers for reflux flow and reboiler heat input are operated manuallyThis work demonstrates the operation of a batch stripping column，provides some practical guidlines for the startup and operation of the column，shows how the column can be run under different operating modes，and clarifies the effect of some key control tuning on the column performance However，this work is a dynamic simulation The practical operation of a batch stripping distillation column still needs to be investigated in detailREFERENCES1 Salomone，HE，Chiotti，OJ，Iribarren，OA，“Shortcutdesign procedure for batch distillation”，IndEng ChenRes，36 (1)，13 一136(1997)2 Sundaram，S，Evans，LB，“Shortcut procedure for simulatingbatch distillation operations”，Ind EI enRes，32(3)，511 518(1993)3 Yang，zhC，Yu，GC(KT )，Mo，zhM，ea， t“Study on optimal strategies and microcomputer control ofbatch distillation()Batch distillation column and its microcomputercontrol”，J(ChemIndEng(China，40(3)，28 一286(1989)(in Chinese) 4 Lotter， S P， Diwekar， U M ， “Shortcut models andfeas ibility consideration for emerging batch distillationcolumns”，IndEngChemRes，36(4)，760767(1997)5 Scrensen，E，Skogestad，S，“Comparison of regular andinverted batch distillation”，Chem Eng Sci，51 (22)，4949一4962 of 1996)分批冲孔模板精馏塔的操控许松林，Jose Espinosab，Hector ESalomoneb，Oscar AIribarrenba 中国 ，天津，300072，天津大学，国家精馏工程技术研究中心b 阿根廷，桑塔费，康尼赛特，INGAR发展与设计学院摘要 当大量的轻的成分在流量中很少和高纯度产品回收时分批冲孔模板精馏很重要，批量精馏塔的操控与镇流器的作用是相同的。然而，冲孔模板的控制系统是不同的。在这篇论文里，我们探索冲孔模板三种不同的控制方法：Hysys(Hyprotech Ltd1997)，最主要的不同之处是重沸器液相控制图；（a）以回流量控制;（b)以重沸器热负载控制；（c）以底部产品流量控制。在此论文里阐述分批冲孔模板精馏塔的操控最主要的特征是不同的控制流程图，分批冲孔模板控制开始时提供了准则，将要讨论一些柱面上的控制调谐参数。 图1分批冲孔模板的控制流程1-塔体；2-重沸器；3-冷却机；4-整流器；LC-液面控制器；PC-压力控制器关键词 分批冲孔模板 控制 操作1 简介随着化工工厂向着大规模精细生产和专业化工产品方向发展，批量生产变得比较流行，这样简易方法对于产品需求的频繁变化起关键作用。批量精馏塔是固有简易特性的，正如一个柱可以由一个多组分供给分成许多不同的组份，这样批量精馏的用途对于一些化学，食品和药物公司的高价值的化工产品的分离和提纯变得越来越重要。 传统的，最流行的批量精馏方法被称为整流柱，它有一个大的重沸器，对它所有的供给都是变化的，并且不同产品从顶部分离开。操作整流塔有三种方法：（1）回流量为恒量并且精馏组份为变量，（2）回流量为变量并且精馏的主要组份为恒量，（3）最佳回流量协调了（1）和（2）并且建立在最经济的试验。 批量冲孔模板与批量整流是相反的。在它的顶端有它的储存容器并且产品从塔的底部分离出。当大量的轻的成分在流量中很少和高纯度产品回收时分批冲孔模板精馏很重要。批量精馏塔的操控与镇流器的作用是相同的。然而，冲孔模板的控制系统是不同的。在论文中，我们探索Hysys(Hyprotech Ltd1997)的批量冲孔模板三种不同的控制方法，图表1给出了控制图。最主要的不同之处是重沸器液相控制图；（a）以回流量控制;（b)以重沸器热负载控制；（c）以底部产品流量控制。 （a）底部产品的组分 （b）塔体中的温度 （c）质量流量 （d）顶部和底部的流量 在此论文里阐述分批冲孔模板精馏塔的操控最主要的特征是不同的控制流程图，分批冲孔模板控制开始时提供了准则，将要讨论一些柱面上的控制调谐参数。 2 模拟实验仪器 模拟实验仪器和三种控制图是相同的，脱模塔有个重沸器和2 m 3和5 m 3的冷凝器，他的直径是0.5m.供给成分是甲醇（0.05）和乙醇（0.95）（馏分）的混合物。占冷凝器容量的80%，开始时，板是干启动的，但是重沸器是由相同的混合液的液相点控制的。底部产品乙醇的规范是0.999.所有的仿真实验程序是从冲模开始直到关键的组份达到规范，然后底部产品阀开启使产品分离，当产品组份低于规范时产品阀关闭。3 结果和讨论3.1 通过回流量控制重沸器液面在控制图中【图表1（a）】,重沸器液相百分比是由回流量自动控制的，重沸器的热输出和底部产品的流量是手动控制的。开始时，重沸器的热输出是设定的，重沸器的液面随着轻成分的蒸发而降低，这将导致回流自动地流向重沸器。重沸器的液面控制是可逆的，所以当重沸器的液面较高时，回流量将较少。当关键组份是成分达到其规范时，底部的阀开启，一旦它低于规范，底部产品流出阀就手动关闭，这样的话，当乙醇成分达到0.999，底部产品流出阀开启，当乙醇成分低于0.999，底部产品流出阀关闭。 图表3重沸器液面的波动图表2表示了此操作模式的动态过程。在重沸器液面和回流之间存在时间滞后，尤其是当阶段数目很大时。为了在整个控制中达到一个稳定的重沸器的液面。必须仔细考虑两个方面。如果回流阀过大，当液面降低时，重沸器的液面控制器将从重沸器得到比预设多的回流量。然后回流阀将会关闭。这使重沸器液面频繁波动。图表3展现出了一种情况，在这种情况底部关键成分的组成是不稳定的，另一方面是重沸器的液相参数
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