浮头式换热器外文翻译
浮头式换热器(过程设备设计课程设计说明书)参考word
目录设计题目及工艺参数---------------------------------------------------1一、换热器的分类及特点---------------------------------------------------2二、结构设计-------------------------------------------------------------51、管径及管长的选择---------------------------------------------------52、初步确定换热管的根数n和管子排列方式-------------------------------53、筒体内径确定-------------------------------------------------------54、浮头管板及钩圈法兰结构设计-----------------------------------------65、管箱法兰、管箱侧壳体法兰和管法兰设计-------------------------------76、外头盖法兰、外头盖侧法兰设计---------------------------------------77、外头盖结构设计-----------------------------------------------------88、接管的选择--------------------------------------------------------------------------------------89、管箱结构设计-------------------------------------------------------810、管箱结构设计------------------------------------------------------811、垫片选择----------------------------------------------------------912、折流板------------------------------------------------------------------------------------------913、支座选取----------------------------------------------------------1014、拉杆的选择--------------------------------------------------------1315、接管高度(伸出长度)确定------------------------------------------1316、防冲板------------------------------------------------------------1317、设备总长的确定----------------------------------------------------1318、浮头法兰---------------------------------------------------------------------------------------1419、浮头管板及钩圈----------------------------------------------------14三、强度计算--------------------------------------------------------------141、筒体壁厚的计算-----------------------------------------------------142、外头盖短节,封头厚度计算-------------------------------------------153、管箱短节、封头厚度计算 --------------------------------------------164、管箱短节开孔补强的核校 --------------------------------------------165、壳体压力试验的应力校核---------------------------------------------166、壳体接管开孔补强校核-----------------------------------------------177、固定管板计算-------------------------------------------------------188、无折边球封头计算 --------------------------------------------------199、管子拉脱力计算-----------------------------------------------------20四、设计汇总-----------------------------------------------------21五、设计体会--------------------------------------------------------------21参考文献--------------------------------------------------------------22设计题目:浮头式换热器工艺参数:管口表:符号公称直径(mm)管口名称a 130 变换气进口b 130 软水出口c 130 变换气出口d 130 软水进口e 50 排尽口设备选择原理及原因:浮头式换热器的结构较复杂,金属材料耗量较大,浮头端出现内泄露不易检查出来,由于管束与壳体间隙较大,影响传热效果。
浮头式换热器英文论文1
Floating-head heat exchangersThe present invention relates to an improvement in floating-head type heat exchangers and particularly to means for providing fluid-tight contact between a floating tube sheet and a head flange such exchangers. More particularly, this invention is concerned with a special packing joint which provides an effective seal between the shell side and the tube side and the tube side of a floating-head type heat exchanger. The use of so-called”shell and tube”heat exchangers has gained widespread commercial acceptance. Such exchangers are useful in transferring heat between two liquids, such as for example, in oil refining operation, or between a liquid and a vapor, such as for example in steam power plants. The relative thermal expansions or contraction which frequently result from differences in the temperatures of the fluids flowing through the tubes and the shell, or from differences in the materials of construction of the tubes and the shells, have led to the development and use of the so-called”floating-head”heat exchangers. In this type of exchanger the tubes are rigidly attached to a stationary tube sheet which is fixed relative to the shell of the exchanger at one end,and are attached to a floating tube sheet at the other end. Hence, in operation,slidable movement obtains between the floating tube sheet and the shell and other fixed parts as the expanding and contracting tubes cause movement of the floating tube sheet, and stress and strains which may otherwise cause wear and failure in the exchanger are therefore avoided.In the shell and tube heat exchangers, one fluid usually enters the shell at one end and discharges from the opposite side of the shell at the other end, or at the same end, depending upon whether a singer-pass or a double-pass arragement of tubes is employed. The other fluid flows through the tubes from one end and is discharged at the other end(single pass flow), or the fluid may flow through part of the tubes at one end,re-routed through another part of the tubes, in which case such arrangement is referred to as multiple pass flow. Indouble-pass flow, for example, the liquid enters half the tubes at one end and flows, say from right to left, discharges into a receiving chamber, and then re-routed to the remaining half of the tubes through which it flows from left to right, and finally discharges from the heat exchanger.It can be readily appreciated that in this type of heat exchanger, provisions must be made to prevent leakage of fluid from the shell side to the tube side or vice versa. Several suchprovisions have been suggested and adapted to these exchanger but they are all disadvantageous in one way or another. Most frequently, the floating-head is either bolted or clamped onto the floating tube-sheet and the entire assembly is then mounted in the shell by means of conventional expansion rings or packing joints. This arragement, however, is expensive, cumbersome and difficult to install and to disassemble.Accordingly, this invetion comprehends and resides in the discovery of novel means for providing fluid-tight contact between the floating tube-sheet and the head flange protion of the floating head heat exchanger. The novel means employed herein comprises two rings, preferably metallic, with packing materials thereon, said rings being separated by compressible and resilient members, such as, for example, spring washers. These washers are arranged each over one of a multiplicity of circumferentially arranged pins extending longitudinally between the rings, fixed to one ring and slidably movable through aligned holes in the other ring. The pins serve to keep the washers in position.The novel means employed in the present invention and its adaptation to the floating-head heat exchanger are more readily comprehended with reference to the attached drawings wherein:FIGURE 1 is a partially sectionalized side elevation of a floating-head type heat exchanger embodying this invention;FIGURE 2 is an enlarged section showing the detials of a floating-head joint of FIGURE 1, and FIGURE 3 is an isometric free-body view of the two rings showing their relative positions with the washers.In these drawings, like numerals designate like parts.Referring to the drawings,there is shown, on thefloating-head side of the heat exchanger, a shell flange 11, gasket 13 and head flang 15, all connected together via bolt 17. Also shown on this side of the exchanger is a floating tube-sheet 19 to which is attached a multiplicity of tubes 21 through which one fluid madium flows. The other fluid medium enters the shell 23 of the exchanger at enrance 25, flows through the shell in contact with the outer surface of tubes 21 and leave the shell at exit 27.Forming a liquid-tight contact between the floating bute-sheet 19, the shell flange 11 and head flange 15 there is shown a unitary structure comprising two metallic rings 29 and 31 which are connected via two or more pins 33. There pins are attached at one end to one of said rings, say,ring 31 by welding or any other suitable means, and at the other end the pins areinserted in apertures in the ring 29 through which the pins are free to move in axial direction. A resilient and compressible member 35, such as,for example, a spring wsaher, is set over each pin, which member is responsive to the relative movements and expansions and contractions at the floating-head joints. Pins 33, apart from their function of connecting the two metal rings, also serve to hold the spring washers in the circumferential array shown.The unitary structure referred to above is placed in a recess 37(or a groove, or a notch) specially cut in the flanges, and the remaining space on either side of the rings is filled with packing materials 39 and 41 to fill up the recess. The diameter of the packing materials is preferably slightly larger than the outside diameter of the two metal rings to provide an effective seal as will hereinafter be explained.Rings 29 and 31 can be of metallic or plastic materials capable of withstanding the compressive forces exerted thereon by the spring washers 39 during the operation of the heat exchanger. The washers 35 may be of any suitable resilient and compressible materials capable of responding to the thermal expansions and contractions resulting from the differences in the temperatures of the fluids flowing through the shell andthe tube, or to differences in the materials of construction of the shell and the tubes. The number washers can very depending upon the compressive forces exerted in the floating-head joint.In assembling the heat exchangher, when bolts 17 are tightened, gasket 13 is compressed between the surfaces of the shell flange 11 and head flange 15. The compressive forces so set up are transmitted to the packing material 39 and 41 which packing material are therefore compressed away from each other as well as against the floating tube-sheet 19 the shell flange 11 and the head flange 15. Thus a fluid-tight contact is provided between the shell side and the tube side of the heat exchanger at floating-head joint. The compressive forces which are so transmitted to the packing matreial are in turn absorbed by the spring washers 35 which remain compressed in response to these compressive forces and which can return to their normal uncompressed position upon the removal of these forces.Thermal expansions and contractions at the floating-head joint,resulting from differences in temperature or differences in the materials of construction, as was previously discussed, cause relative movement of the floating tube-sheet 19 with respect to the shell flange 11 and head flange 15. The noveldevice permits the tube sheet to slide against the surfaces of the shell flange and the head flange and at the same time provides a seal between the shell side and the tube side of the exchanger.The device of this invention can be employed in single-pass as well as multiple-pass heat exchangers. It offers simplicity of installation as well as disassemblement of the exchanger and is less costly than the heretofore common types of installations.What is claimed is:1.In a floating-head heat exchanger having a flanged shelland a flanged head cover for said shell providingtherewith an annular recess at the juncture of the shelland cover, a tube bundle in said shell, a floating tubesheet slidably supporting one end of said tube bundleand having an annular surface facing said recess, a fluidtight sealing means disposed in said annular recesscomprising a pair of sealing ring members, spring meansbetween said sealing ring menbers resiliently biasingthe same apart and into engagement with the end wallsof said annular recess, said sealing ring members eachbeing in sealing engagement with the annular surface ofsaid tube sheet and the bottom of said recess andproviding a seal between the same and the shell and said spring means permitting said sealing rings to react resiliently in response to longitudinal movement of said floating tube sheet.2.In a floating-head heat exchanger having a flanged shelland a flanged head cover for said shell providingtherewith an annular recess at the juncture of the shell and cover, a tube bundle in said shell, a floating tube sheet slidably supporting one end of said tube bundle and having an annular surface facing said recess, a fluid-tight sealing means disposed in said recesscomprising a pair of oppositely disposed spaced rings, resilient means mounted by and between said rings urging the same axially apart, packing members between each of said rings and the adjacent surfaces of said recess ,said packing members being of slightly larger diameter than the rings and bearing on the floating tube sheet and the opposed suefaces of said recess to provide a seal between the tube sheet and the shell and to provide a seal between the tube sheet and the shell and to permit said sealing members to react resiliently responsive to longitudinalmovement of said floating tube sheet.。
浮头式换热器外文翻译
自由对流热转移反响从垂直加热板到地表热通量的振荡马侯赛因和SK达斯,孟加拉国达卡和DAS里斯,英国巴斯〔收稿,1996年6月3日~1996年7月12日修订〕总结进展调查的二维不稳定层流沿半无限的竖直板和对流边界的粘性不可压缩流体的层流平均地表热通量关于稳定姿态的小幅度振荡。
浮力是有利的,从积极的热通量板外表的流体与往常边界层流的时间周期热通量的互相作用满足审查线性理论。
解决方案是利用三种不同的方法,即扩展的一系列扩大低频,高频渐近级数展开法和一般频率的数值有限差分法已经进展了广泛的参数计算,以便找到在波动的幅度和相位角的解决方案。
人们已经发现,振幅和相位角,零件外表的剪切应力和外表温度,这三种方法的预测是非常好的在各自有效期的范围。
11介绍在层流边界层理论的领域,莱特希尔[1]是第一个研究的不稳定平板和圆柱与被迫流动的粘性不可压缩流体的自由流,有小幅度的振荡。
自由对流的相似性解决方案从外表均匀热通量与垂直板最初量是研究麻雀格雷格[2]和获得附近的领先优势有效的解决方案。
相应的问题是非定常对流沿垂直板外表温度振荡由纳达和夏尔马[3]和Eshghy等研究。
[4]。
muhuri和梅蒂[5]和Verma[6]分析了非定常自由对流的振荡外表温度的影响。
所有这些调查是基于这样的假设,外表温度执行与时间有关的小振幅振荡意味着温度,和他们进展了通过采用卡门Pohlhausen 近似的积分法。
为了获得有效的领先优势,在附近的摄动解下游地区,罗伊[7]认为是高普朗特数的同类型的问题,威尔克斯[8]研究了一个统一的外表热通量垂直板自由对流的问题。
在规定的地表热通量的垂直板的情况下,研究由梅尔金和Mahmood[,乔杜里和梅尔金[11]等人。
这些作品被源源不断局限,使解决方案得到了有效的间隔,解决方案也给出了中间区域。
基于对线性化理论,凯莱赫和杨[12]研究了层流换热反响逃离对流边界层沿垂直加热板外表温度振荡的问题,最近,侯赛因等调查同类型的问题,详细的外表平均温度,θω〔x〕,“其中x与该板块的领先优势的流向间隔成正比。
换热器简介
填料函式&滑动管板换热 器
因填料处易产生泄漏,填料函 式换热器一般适用于4MPa以下的工 作条件,且不适用于易挥发、易燃、 易爆、有毒及贵重介质,使用温度 也受填料的物性限制。填料函式换 热器现在已很少采用。
双管板&薄管板换热器
管板是管壳式换热器的最重要部件 之一
避免冷热流体混合,并同时受管程, 壳程压力和温度的作用,要求连接 强度和密封性。 双管板有利于防止一侧流体向另一 侧流体的泄漏 双管板防止壳程和管程流体严禁混 合的情况 薄管:管板厚了热应力 能力差 管板薄了 耐压性能差
换 热 器
ቤተ መጻሕፍቲ ባይዱ换热器(英语翻译:heat exchanger),是 将热流体的部分热量传递给冷流体的设备, 又称热交换器。
换热器分类
/
换热器的选用
考虑因素: 流体的性质,压力, 温度, 压降, 可调范围; 清洗维修的要求, 现场安装和检修的方便程度,使用寿命和可靠性 满足几点要求: 1,给定的工作条件下。达到要求的传热量和流体出口温度 2,流体压降要小,减少运行的能量消耗。 3,满足场地的要求和重量要求 4,防腐,防漏。容易维修。工作寿命等安全可靠 5,选材合理且来源有保证,以减少投资 6,安装运输,等
板式换热器
优点: 换热效率高 针对性强 结构紧凑 适应力强 热损失小
缺点 耐压性能差 工作温度较低 容易泄漏 可拆式 :密封垫片 焊接式 :完了就全完了板片全焊接 上 半焊接式:密封垫 & 焊接 钎焊式:使用面积小,耐温压,完= 完 板壳式:耐温耐压,传热系数是管 壳的2倍
板片
人字波 平直波 球形波 浅波纹 非对称
换热器之管壳式
1, 固定管板式换热 器 2, 浮头式换热器 3,U形管换热器 4,填料函式换热器 5,滑动管板换热器 6,双管板换热器 7,薄管板换热器
浮头式换热器
浮头式换热器浮头式换热器是一种常见的热交换设备,被广泛应用于化工、石油、电力、制药等工业领域。
它具有结构简单、换热效果好、运行稳定等特点,在工业生产中发挥着重要的作用。
浮头式换热器的设计原理是利用两种不同介质之间的传热,以实现能量的转移。
它由壳体、束管板、浮头和传热管等组成。
其中,壳体是外部的固定壳体,束管板分隔开了两种介质,传热管是主要传热介质,而浮头则可以随着流体的膨胀和收缩而自由移动。
浮头式换热器的工作过程如下:首先,将需要传热的介质注入传热管中,同时通过固定壳体的入口和出口进行连通。
然后,热能从传热管中传到固定壳体中的冷介质上,由冷介质通过出口流出,实现了热量的传递。
在整个过程中,浮头会根据传热管内外温度的差异而产生膨胀和收缩,以保持壳体内部的良好密封性能。
浮头式换热器的设计和选型,需要考虑多个因素。
首先是流体的性质和流量。
不同的流体有不同的传热特性,所以在选择传热器时需要考虑流体的温度、压力、粘度等参数。
其次是传热器的传热效率。
传热效率是评价换热器性能的重要指标,因此在设计过程中需要合理选择传热面积、传热管的材质和数量等。
最后是换热器的安装和维护。
浮头式换热器通常较大,所以在安装时需要考虑到空间和结构的限制。
而维护方面,需要定期检查传热管内壁的结垢情况,及时清洗和维修。
浮头式换热器在工业生产中具有广泛的应用。
它能够实现不同介质之间的热量传递,有效利用能源,提高生产效率。
同时,由于浮头的作用,它还能够适应介质的膨胀和收缩,减少了由于温度变化引起的应力和振动,保证了设备的安全稳定运行。
总的来说,浮头式换热器是一种重要的热交换设备,在工业生产中起着关键的作用。
它采用简单的结构设计,具有良好的传热效果和稳定的运行性能,能够满足不同介质之间的热量传递需求。
随着工业技术的发展,浮头式换热器的设计和制造技术也在不断改进和创新,为工业生产提供更加可靠和高效的换热解决方案。
浮头式换热器PN1.6DN500
摘要本设计说明书介绍了题目为PN1.6DN500冷却器的设计过程,并简要论述了它的运用场合、特点和制造加工工艺。
本文首先以给出的技术特性与工艺参数为基础,利用传热原理等理论进行工艺计算,确定了内导流浮头式冷却器的基本型号BES 500—1.6—55—3/19—2Ⅱ;再依据GB150—1998《钢制压力容器》和GB151—1999《管壳式换热器》等标准着重对浮头式换热器各零部件进行了结构设计与强度校核,包括筒体、管箱、浮头法兰、浮头盖、管板以及开孔补强等部件及元件;最后,介绍了内导流浮头式换热器的检验、安装、使用与维修等内容。
关键词:传热系数内导流筒浮头法兰弓形折流板浮头式换热器AbstractThis design specifications introduces the design process of PN1.6 DN500 cooler, and expounds briefly the utilization situation、characteristic and manufacture process. Firstly, It is based on physical technical characteristic and technology parameter given in the production that the technology calculation is done by making use of fundamentals about heat transfer process in order to define the model of floating-head type cooler with inner diversion tube,which is BES 500—1.6—44.9—3/25—2Ⅱ. Then, the structural design and intensity examination about most of components in heat exchanger are carried out by means of standards, such as GB150—1998<Steel pressure vessels> and GB151—1999<shell and tube heat exchanger>,including tube body、tube box、floating head flange、floating head cover、the tube plate as well as reinforcement for opening and so on. Finally, it is also related to inspection、installation、operation and maintenance about floating-head type heat exchanger with inner diversion tube.Key word: heat transfer coefficient ;inner diversion tube ; floating head flange;flow resistance;segmental baffle;floating-head type heat exchanger ;目录摘要 (I)Abstract....................................................... I I 绪论. (1)第一章方案论证 (5)1.2 经济合理性 (7)1.3 结构可操作性 (7)第二章结构及强度设计 (9)2.1 筒体结构设计及计算[1] (9)2.1.1. 筒体厚度计算 (9)2.1.2 筒体的强度校核和水压试验 (10)2.2 管箱结构设计 (11)2.2.1封头的材料及形式选择[14] (11)2.2.2标准封头壁厚计算 (11)2.2.3管箱应力校核 (12)2.2.4 管箱的结构设计 (12)2.3 管箱法兰设计 (13)2.3.1 法兰选用[5] (13)2.3.2垫片选用[8] (13)2.3.3螺柱与螺母选用[5] (14)2.3.4管箱法兰计算及校核[2] (14)2.4 钩圈式浮头的设计 (19)2.4.1 钩圈式浮头的结构尺寸计算 (19)2.4.2 浮头盖的设计计算 (20)2.4.3浮头钩圈的设计计算 (28)2.5 换热管及管板的设计 (28)2.5.1、换热管的设计 (28)2.5.2 换热器管板设计 (30)2.6 外头盖设计 (35)2.6.1 外头盖侧法兰选用[10] (35)2.6.2.外头盖法兰选用[5] (36)2.6.3.外头盖垫片及其它[9] (36)2.6.4 外头盖封头的设计[14] (36)2.7 开孔补强设计[1] (37)3.7.1 补强判别 (37)2.7.3.封头开孔补强计算 (39)2.8 其他零部件设计[2] (40)2.8.1拉杆设计 (40)2.8.2 分程隔板设计 (41)2.8.3 定距管设计 (41)2.8.4滑道设计 (41)2.8.5 折流板的设计计算 (41)P) (43)2.8.6. 防冲板设计(GB151- 1999,762.8.7. 内导流筒的选用 (43)2.8.8. 防短路结构设计 (43)2.8.9. 鞍式支座的选用[11] (44)2.8.10. 预防管束发生振动破坏的措施 (45)第三章浮头式换热器的制造、检验与验收 (46)3.1浮头式换热器制造、检验与验收要求 (46)3.2浮头式换热器的制造工艺[4] (46)3.2.1主要零部件的加工工艺 (46)3.2.3 浮头式换热器的焊接工艺 (49)3.2.4 浮头式换热器的涂漆工艺 (51)3.3浮头式换热器的检验与验收 (51)3.3.1 换热器常见的试验工艺及要求 (52)3.3.2 浮头式换热器的检验工艺 (52)第四章浮头式换热器的安装、使用与维修 (54)4.1浮头式换热器的安装要求 (54)4.2浮头式换热器的使用与维修[4] (54)4.2.1浮头式换热器使用时常见的几种破坏形式 (54)4.2.2浮头式换热器的维修 (55)第五章分析与总结 (56)设计小结 (57)参考文献 (58)致谢 (59)绪论过程设备在生产技术领域中应用非常广泛,是化工、炼油、轻工、交通、食品、制药、冶金、能源、纺织、宇航、城建、国防、海洋工程等传统部门所必需的关键设备。
管壳式换热器的有效设计-外文翻译
武汉工程大学邮电与信息工程学院毕业设计(论文)外文资料翻译原文题目: Effectively Design Shell-and-Tube Heat Exchangers 原文来源: Chemical Engineering ProgressFebruary 1998文章译名:管壳式换热器的优化设计姓名: xxx学号: xx指导教师(职称):王成刚(副教授)专业:过程装备与控制工程班级: 03班所在学院:机电学部管壳式换热器的优化设计为了充分利用换热器设计软件,我们需要了解管壳式换热器的分类、换热器组件、换热管布局、挡板、压降和平均温差。
管壳式换热器的热设计是通过复杂的计算机软件完成的。
然而,为了有效使用该软件,需要很好地了解换热器设计的基本原则。
本文介绍了传热设计的基础,涵盖的主题有:管壳式换热器组件、管壳式换热器的结构和使用范围、传热设计所需的数据、管程设计、壳程设计、换热管布局、挡板、壳程压降和平均温差。
关于换热器管程和壳程的热传导和压力降的基本方程已众所周知。
在这里,我们将专注于换热器优化设计中的相关应用。
后续文章是关于管壳式换热器设计的前沿课题,例如管程和壳程流体的分配、多壳程的使用、重复设计以及浪费等预计将在下一期介绍。
管壳式换热器组件至关重要的是,设计者对管壳式换热器功能有良好的工作特性的认知,以及它们如何影响换热设计。
管壳式换热器的主要组成部分有:壳体封头换热管管箱管箱盖管板折流板接管其他组成部分包括拉杆和定距管、隔板、防冲挡板、纵向挡板、密封圈、支座和地基等。
管式换热器制造商协会标准详细介绍了这些不同的组成部分。
管壳式换热器可分为三个部分:前端封头、壳体和后端封头。
图1举例了各种结构可能的命名。
换热器用字母编码描述三个部分,例如, BFL 型换热器有一个阀盖,双通的有纵向挡板的壳程和固定的管程后端封头。
根据结构固定管板式换热器:固定管板式换热器(图2)内装有直的换热管,这些管束两端固定在管板上,管板则被焊接在壳体上。
浮头式换热器设计说明书
1 绪论1.1 换热设备在工业中的应用在炼油、化工生产中,绝大多数的工艺过程都有加热、冷却和冷凝的过程,这些过程总称为换热过程。
传热过程的进行需要一定的设备来完成,这些使传热过程得以实现的设备就称之为换热设备。
据统计,在炼油厂中换热设备的投资占全部工艺设备总投资的35%~40%,因为绝大部分的化学反应或传质传热过程都与热量的变化密切相关,如反应过程中:有的要放热、有的要吸热、要维持反应的连续进行,就必须排除多余的热量或补充所需的热量。
工艺过程中某些废热或余热也需要加以回收利用,以降低成本。
综上所述,换热设备是炼油、化工生产中不可缺少的重要设备。
换热设备在动力、原子能、冶金及食品等其他工业部门也有着广泛的应用。
1.2 换热设备的分类1.2.1按作用原理或传热方式可分为:直接接触式、蓄热式、间壁式。
1.2.1.1直接接触式换热器,如下图所示热流体图1.1其传热的效果好,但不能用于发生反应或有影响的流体之间。
蓄热式换热器,如下图所示图1.2其适用于温度较高的场合,但有交叉污染,温度被动大。
1.2.1.3 间壁式换热器,又称表面式换热器利用间壁进行热交换。
冷热两种流体隔开,互不接触,热量由热流体通过间壁传递给冷流体。
1.2.2 按其工艺用途可分为:冷却器(cooler)、冷凝器(condenser)、加热器(一般不发生相变)(heater)、蒸发器(发生相变)(evaporator)、再沸器(reboiler)、废热锅炉(waste heat boiler)。
1.2.3 按材料分类:分为金属材料和非金属材料换热器。
1.3 国内外的研究现状上个世纪70年代初发生世界性能源危机,有力地促进了传热强化技术的发展。
为了节能降耗,提高工业生产的经济效益,要求开发适用不同工业过程要求的高效能换热设备。
因此,几十年来,高效换热器的开发与研究始终是人们关注的课题,国内外先后推出了一系列新型高效换热器。
近年来,国内已经进行了大量的强化传热技术的研究,但在新型高效换热器的开发方面与国外差距仍然较大,并且新型高效换热器的实际推广和应用仍非常有限。
浮头式换热器计算说明书
设备设计说明书
目 录
AES 浮头式换热器的设计............................................................................................................................ 1 第 1 章 概述................................................................................................................................................. 1 第 1·1 节 设备的简介................................................................................................................................1 第 1·2 节 设备的基本结构......................................................................................................................3 第 2 章 结构设计......................................................................................................................................... 4 第 2·1 节 材料的选择................................................................................................................................4 第 2·2 节 主要结构设计............................................................................................................................7 第 3 章 设计计算......................................................................................................................................... 8 第 3·1 节 筒体及封头壁厚计算................................................................................................................8 第 3·2 节 管板计算..................................................................................................................................13 第 3·3 节 浮头法兰计算..........................................................................................................................19 第 3·4 节 钩圈计算..................................................................................................................................22 第 3·5 节 球冠形封头计算......................................................................................................................22 第 3·6 节 开孔补强计算..........................................................................................................................22 第 3·7 节 鞍座支反力计算..................................................................................... 错误!未定义书签。 第 4 章 制造、安装与检验.....................................................................................................................28 第 5 章 经济性分析................................................................................................................................. 33 结论............................................................................................................................................................. 34 参考文献..................................................................................................................................................... 35 符号说明..................................................................................................................................................... 36 致谢............................................................................................................................................................. 38
浮头式换热器的设计PNDN600
浮头式换热器的设计PNDN600摘要 (1)Abstract (2)前言 (3)第一章换热器概述 (4)1.1 换热器的应用 (4)1.2 换热器的要紧分类 (4)1.3 管壳式换热器专门结构 (10)1.4 换热管简介 (11)第二章工艺运算 (12)2.1 设计条件 (12)2.2 核算换热器传热面积 (12)2.3 压力降的运算 (18)2.4 换热器壁温运算 (20)第三章换热器结构设计与强度运算 (23)3.1 壳体与管箱厚度的确定 (23)3.2 开孔补强运算 (25)3.3 水压试验 (31)3.4 换热管 (32)3.5 管板设计 (34)3.6 折流板 (40)3.7 拉杆与定距管 (42)3.8 防冲板 (43)3.9 保温层 (43)3.10法兰与垫片 (44)3.11 钩圈式浮头 (47)3.12 分程隔板 (53)3.13 鞍座 (54)3.14 接管的最小位置 (55)第四章换热器的腐蚀、制造与检验 (57)4.1 换热器的腐蚀 (57)4.2 换热器的制造与检验 (58)第五章焊接工艺评定 (61)5.1 壳体焊接工艺 (61)5.2 换热管与管板的焊接 (62)5.3 法兰与筒体的焊接 (62)第六章换热器的安装、试车与爱护 (63)6.1 安装 (63)6.2 试车 (64)6.3 爱护 (64)总结 (65)致谢 ...................................... 错误!未定义书签。
参考文献 (67)附录Ⅰ浮头法兰厚度运算程序 (68)附录Ⅱ相关文献 (72)摘要本设计说明书是关于PN2.5DN600浮头式换热器的设计,要紧是进行了换热器的工艺运算、换热器的结构和强度设计。
设计的前半部分是工艺运算部分,要紧是依照给定的设计条件估算换热面积,从而进行换热器的选型,校核传热系数,运算出实际的换热面积,最后进行压力降和壁温的运算。
设计的后半部分则是关于结构和强度的设计,要紧是依照差不多选定的换热器型式进行设备内各零部件(如接管、折流板、定距管、钩圈、管箱等)的设计,包括:材料的选择、具体尺寸确定、确定具体位置、管板厚度的运算、浮头盖和浮头法兰厚度的运算、开孔补强运算等。
浮头式换热器
浮头式换热器浮头式换热器简介浮头式换热器两端的管板,一端不与壳体相连,该端称浮头。
管子受热时,管束连同浮头可以沿轴向自由伸缩,除去了温差应力。
浮头式换热器结构浮头式换热器结构在凹型和梯型凹槽之间钻孔并套丝或焊设多个螺杆均布,设浮头法兰为凸型和梯型凸台双密封,分程隔板与梯型凸台相通并位于同一端面的宽面法兰,且凸型和梯型凸台及分程隔板分别与浮头管板凹型和梯型凹槽及分程凹槽相对应匹配,该浮头法兰与无折边球面封头组配焊接为浮头盖,其法兰螺孔与浮头管板的丝孔或螺杆相组配,用螺栓或螺帽紧固压紧浮头管板凹型和梯型凹槽及分程凹槽及其垫片,该结构必须时可适当加大浮头管板的厚度和直径及圆筒的内径,同时相应更改加大相关零部件的尺寸;另配置一无外力辅佑襄助钢圈,其圈体内径大于浮头管板外径,钢圈一端设法兰与外头盖侧法兰内侧面凹型或梯型密封面连接并密封,另一端设法兰或其他结构与浮头管板原凹型槽及其垫片或外圆密封。
浮头式换热器设计要求浮头式换热器随着经济的进展,各种不同型式和种类的换热器进展很快,新结构、新料子的换热器不绝涌现。
为了适应进展的需要,中国对某些种类的换热器已经建立了标准,形成了系列。
完善的换热器在设计或选型时应充足以下基本要求:(1)合理地实现所规定的工艺条件;(2)结构安全牢靠;(3)便于制造、安装、操作和维护和修理;(4)经济上合理。
浮头式换热器的一端管板与壳体固定,而另一端的管板可在壳体内自由浮动,壳体和管束对膨胀是自由的,故当两种介质的温差较大时,管束和壳体之间不产生温差应力。
浮头端设计成可拆结构,使管束能简单的插入或抽出壳体。
(也可设计成不可拆的)。
这样为检修、清洗供给了便利。
但该换热器结构较多而杂,而且浮动端小盖在操作时无法知道泄露情况。
因此在安装时要特别注意其密封。
浮头换热器的浮头部分结构,按不同的要求可设计成各种形式,除必须考虑管束能在设备内自由移动外,还必须考虑到浮头部分的检修、安装和清洗的便利。
换热器外文翻译 (2)
Heat ExchangersKey Terms Baffles—evenly spaced partitions in a shell and tube heat exchanger that support the tubes, prevent vibration, control fluid velocity and direction, increase turbulent flow, and reduce hot spots. Channel head—a device mounted on the inlet side of a shell-and-tube heat exchanger that is used to channel tube-side flow in a multipass heat exchanger.Condenser—a shell-and-tube heat exchanger used to cool and condense hot vapors.Conduction—the means of heat transfer through a solid, nonporous material resulting from molecular vibration. Conduction can also occur between closely packed molecules.Convection—the means of heat transfer in fluids resulting from currents. Counterflow—refers to the movement of two flow streams in opposite directions; also called countercurrent flow.Crossflow—refers to the movement of two flow streams perpendicular to each other.Differential pressure—the difference between inlet and outlet pressures; represented as ΔP, or delta p.Differential temperature—the difference between inlet and outlet temperature; represented as ΔT, or delta t.Fixed head—a term applied to a shell-and-tube heat exchanger that has the tube sheet firmly attached to the shell.Floating head—a term applied to a tube sheet on a heat exchanger that is not firmly attached to the shell on the return head and is designed to expand (float) inside the shell as temperature rises. Fouling—buildup on the internal surfaces of devices such as cooling towers and heat exchangers, resulting in reduced heat transfer and plugging.Kettle reboiler—a shell-and-tube heat exchanger with a vapor disengaging cavity, used to supply heat for separation of lighter and heavier components in a distillation system and to maintain heat balance. Laminar flow—streamline flow that is more or less unbroken; layers of liquid flowing in a parallel path.Multipass heat exchanger—a type of shell-and-tube heat exchanger that channels the tubeside flow across the tube bundle (heating source) more than once.Parallel flow—refers to the movement of two flow streams in the same direction; for example, tube-side flow and shell-side flow in a heat exchanger; also called concurrent.Radiant heat transfer—conveyance of heat by electromagnetic waves from a source to receivers.Reboiler—a heat exchanger used to add heat to a liquid that was onceboiling until the liquid boils again.Sensible heat—heat that can be measured or sensed by a change in temperature.Shell-and-tube heat exchanger—a heat exchanger that has a cylindrical shell surrounding a tube bundle.Shell side—refers to flow around the outside of the tubes of ashell-and-tube heat exchanger. See also Tube side.Thermosyphon reboiler—a type of heat exchanger that generates natural circulation as a static liquid is heated to its boiling point.Tube sheet—a flat plate to which the ends of the tubes in a heat exchanger are fixed by rolling, welding, or both.Tube side—refers to flow through the tubes of a shell-and-tube heat exchanger; see Shell side.Turbulent flow—random movement or mixing in swirls and eddies of a fluid. Types of Heat Exchangers换热器的类型Heat transfer is an important function of many industrial processes. Heat exchangers are widely used to transfer heat from one process to another.A heat exchanger allows a hot fluid to transfer heat energy to a cooler fluid through conduction and convection. A heat exchanger provides heating or cooling to a process. A wide array of heat exchangers has been designed and manufactured for use in the chemical processing industry. In pipe coil exchangers, pipe coils are submerged in water or sprayed with water to transfer heat. This type of operation has a low heat transfer coefficient and requires a lot of space. It is best suited for condensing vapors with low heat loads.The double-pipe heat exchanger incorporates a tube-within-a-tube design. It can be found with plain or externally finned tubes. Double-pipe heat exchangers are typically used in series-flow operations in high-pressure applications up to 500 psig shell side and 5,000 psig tube side.A shell-and-tube heat exchanger has a cylindrical shell that surrounds a tube bundle. Fluid flow through the exchanger is referred to as tubeside flow or shell-side flow. A series of baffles support the tubes, direct fluid flow, increase velocity, decrease tube vibration, protect tubing, and create pressure drops.Shell-and-tube heat exchangers can be classified as fixed head, single pass; fixed head, multipass; floating head, multipass; or U-tube.On a fixed head heat exchanger (Figure 7.1), tube sheets are attached to the shell. Fixed head heat exchangers are designed to handle temperature differentials up to 200°F (93.33°C). Thermal expansion prevents a fixed head heat exchanger from exceeding this differential temperature. It is best suited for condenser or heater operations.Floating head heat exchangers are designed for high temperature differentia is above 200°F (93.33°C).During operation, one tube sheet is fixed and the other “floats” inside the shell.The floatingend is not attached to the shell and is free toexpand.Figure 7.1 Fixed Head Heat ExchangerReboilers are heat exchangers that are used to add heat to a liquid that was once boiling until the liquid boils again. Types commonly used in industry are kettle reboilers and thermosyphon reboilers.Plate-and-frame heat exchangers are composed of thin, alternating metal plates that are designed for hot and cold service. Each plate has an outer gasket that seals each compartment. Plate-and-frame heat exchangers have a cold and hot fluid inlet and outlet. Cold and hot fluid headers are formed inside the plate pack, allowing access from every other plate on the hot and cold sides. This device is best suited for viscous or corrosive fluid slurries. It provides excellent high heat transfer. Plate-and-frame heat exchangers are compact and easy to clean. Operating limits of 350 to 500°F (176.66°C to 260°C) are designed to protect the internal gasket. Because of the design specification, plate-and-frame heat exchangers are not suited for boiling and condensing. Most industrial processes use this design in liquid-liquid service.Air-cooled heat exchangers do not require the use of a shell in operation. Process tubes are connected to an inlet and a return header box. The tubes can be finned or plain. A fan is used to push or pull outside air over the exposed tubes. Air-cooled heat exchangers are primarily used in condensing operations where a high level of heat transfer is required.Spiral heat exchangers are characterized by a compact concentric design that generates high fluid turbulence in the process medium. As do otherexchangers, the spiral heat exchanger has cold-medium inlet and outlet and a hot-medium inlet and outlet. Internal surface area provides the conductive transfer element. Spiral heat exchangers have two internal chambers.The Tubular Exchanger Manufacturers Association (TEMA) classifies heat exchangers by a variety of design specifications including American Society of Mechanical Engineers (ASME) construction code, tolerances, and mechanical design:●Class B, Designed for general-purpose operation (economy and compactdesign)●Class C. Designed for moderate service and general-purpose operation(economy and compact design)●Class R. Designed for severe conditions (safety and durability) Heat Transfer and Fluid FlowThe methods of heat transfer are conduction, convection, and radiant heat transfer (Figure 7.2). In the petrochemical, refinery, and laboratory environments, these methods need to be understood well. A combination of conduction and convection heat transfer processes can be found in all heat exchangers. The best conditions for heat transfer are large temperature differences between the products being heated and cooled (the higher the temperature difference, the greater the heat transfer), high heating or coolant flow rates, and a large cross-sectional area of the exchanger.ConductionHeat energy is transferred through solid objects such as tubes, heads,baffles, plates, fins, and shell, by conduction. This process occurs when the molecules that make up the solid matrix begin to absorb heat energy from a hotter source. Since the molecules are in a fixed matrix and cannot move, they begin to vibrate and, in so doing, transfer the energy from the hot side to the cooler side.ConvectionConvection occurs in fluids when warmer molecules move toward cooler molecules. The movement of the molecules sets up currents in the fluid that redistribute heat energy. This process will continue until the energy is distributed equally. In a heat exchanger, this process occurs in the moving fluid media as they pass by each other in the exchanger. Baffle arrangements and flow direction will determine how this convective process will occur in the various sections of the exchanger.Radiant Heat TransferThe best example of radiant heat is the sun’s warming of the earth. The sun’s heat is conveyed by electromagnetic waves. Radiant heat transfer is a line-of-sight process, so the position of the source and that of the receiver are important. Radiant heat transfer is not used in a heat exchanger.Laminar and Turbulent FlowTwo major classifications of fluid flow are laminar and turbulent (Figure 7.3). Laminar—or streamline—flow moves through a system in thin cylindrical layers of liquid flowing in parallel fashion. This type of flow will have little if any turbulence (swirling or eddying) in it. Laminar flow usually exists atlow flow rates. As flow rates increase, the laminar flow pattern changes into a turbulent flow pattern. Turbulent flow is the random movement or mixing of fluids. Once the turbulent flow is initiated, molecular activity speeds up until the fluid is uniformly turbulent.Turbulent flow allows molecules of fluid to mix and absorb heat more readily than does laminar flow. Laminar flow promotes the development of static film, which acts as an insulator. Turbulent flow decreases the thickness of static film, increasing the rate of heat transfer. Parallel and Series FlowHeat exchangers can be connected in a variety of ways. The two most common are series and parallel (Figure 7.4). In series flow (Figure 7.5), the tube-side flow in a multipass heat exchanger is discharged into the tubeside flow of the second exchanger. This discharge route could be switched to shell side or tube side depending on how the exchanger is in service. The guiding principle is that the flow passes through one exchanger before it goes to another. In parallel flow, the process flow goes through multiple exchangers at the same time.Figure 7.5 Series Flow Heat ExchangersHeat Exchanger EffectivenessThe design of an exchanger usually dictates how effectively it can transfer heat energy. Fouling is one problem that stops an exchanger’s ability to transfer heat. During continual service, heat exchangers do not remain clean. Dirt, scale, and process deposits combine with heat to form restrictions inside an exchanger. These deposits on the walls of the exchanger resist the flow that tends to remove heat and stop heat conduction by i nsulating the inner walls. An exchanger’s fouling resistance depends on the type of fluid being handled, the amount and type of suspended solids in the system, the exchanger’s susceptibility to thermal decomposition, and the velocity and temperature of the fluid stream. Fouling can be reduced by increasing fluid velocity and lowering the temperature. Fouling is often tracked and identified usingcheck-lists that collect tube inlet and outlet pressures, and shell inlet and outlet pressures. This data can be used to calculate the pressure differential or Δp. Differential pressure is the difference between inlet and outlet pressures; represented as ΔP, or delta p. Corrosion and erosion are other problems found in exchangers. Chemical products, heat, fluid flow, and time tend to wear down the inner components of an exchanger. Chemical inhibitors are added to avoid corrosion and fouling. These inhibitors are designed to minimize corrosion, algae growth, and mineral deposits.Double-Pipe Heat ExchangerA simple design for heat transfer is found in a double-pipe heat exchanger.A double-pipe exchanger has a pipe inside a pipe (Figure 7.6). The outside pipe provides the shell, and the inner pipe provides the tube. The warm and cool fluids can run in the same direction (parallel flow) or in opposite directions (counterflow or countercurrent).Flow direction is usually countercurrent because it is more efficient. This efficiency comes from the turbulent, against-the-grain, stripping effect of the opposing currents. Even though the two liquid streams never come into physical contact with each other, the two heat energy streams (cold and hot) do encounter each other. Energy-laced, convective currents mix within each pipe, distributing the heat.In a parallel flow exchanger, the exit temperature of one fluid can only approach the exit temperature of the other fluid. In a countercurrent flowexchanger, the exit temperature of one fluid can approach the inlet temperature of the other fluid. Less heat will be transferred in a parallel flow exchanger because of this reduction in temperature difference. Static films produced against the piping limit heat transfer by acting like insulating barriers.The liquid close to the pipe is hot, and the liquid farthest away from the pipe is cooler. Any type of turbulent effect would tend to break up the static film and transfer heat energy by swirling it around the chamber. Parallel flow is not conducive to the creation of turbulent eddies. One of the system limitations of double-pipe heat exchangers is the flow rate they can handle. Typically, flow rates are very low in a double-pipe heat exchanger, and low flow rates are conducive to laminar flow. Hairpin Heat ExchangersThe chemical processing industry commonly uses hairpin heat exchangers (Figure 7.7). Hairpin exchangers use two basic modes: double-pipe and multipipe design. Hairpins are typically rated at 500 psig shell side and 5,000 psig tube side. The exchanger takes its name from its unusual hairpin shape. The double-pipe design consists of a pipe within a pipe. Fins can be added to the internal tube’s external wall to increase heat transfer. The multipipe hairpin resembles a typical shell-and-tube heat exchanger, stretched and bent into a hairpin.The hairpin design has several advantages and disadvantages. Among its advantages are its excellent capacity for thermal expansion because of its U-tube type shape; its finned design, which works well with fluids that have a low heat transfer coefficient; and its high pressure on the tube side. In addition, it is easy to install and clean; its modular design makes it easy to add new sections; and replacement parts are inexpensive and always in supply. Among its disadvantages are the facts that it is not as cost effective as most shell-and-tube exchangers and it requires special gaskets.Shell-and-Tube Heat ExchangersThe shell-and-tube heat exchanger is the most common style found inindustry. Shell-and-tube heat exchangers are designed to handle high flow rates in continuous operations. Tube arrangement can vary, depending on the process and the amount of heat transfer required. As the tube-side flow enters the exchanger—or “head”—flow is directed into tubes that run parallel to each other. These tubes run through a shell that has a fluid passing through it. Heat energy is transferred through the tube wall into the cooler fluid. Heat transfer occurs primarily through conduction (first) and convection (second). Figure 7.8 shows a fixed head,single-pass heat exchanger.Fluid flow into and out of the heat exchanger is designed for specific liquid–vapor services. Liquids move from the bottom of the device to the top to remove or reduce trapped vapor in the system. Gases move from top to bottom to remove trapped or accumulated liquids. This standard applies to both tube-side and shell-side flow.Plate-and-Frame Heat ExchangersPlate-and-frame heat exchangers are high heat transfer and high pressure drop devices. They consist of a series of gasketed plates, sandwiched together by two end plates and compression bolts (Figures 7.20 and 7.21). The channels between the plates are designed to create pressure drop and turbulent flow so high heat transfer coefficients can be achieved.The openings on the plate exchanger are located typically on one of the fixed-end covers.As hot fluid enters the hot inlet port on the fixed-end cover, it is directed into alternating plate sections by a common discharge header. The header runs the entire length of the upper plates. As cold fluid enters the countercurrent cold inlet port on the fixed-end cover, it is directed into alternating plate sections. Cold fluid moves up the plates while hot fluid drops down across the plates. The thin plates separate the hot and cold liquids, preventing leakage. Fluid flow passes across the plates one time before entering the collection header. The plates are designed with an alternating series of chambers. Heat energy is transferred through the walls of the plates by conduction and into the liquid by convection. The hot and cold inlet lines run the entire length of the plate heater and function like a distribution header. The hot and cold collection headers run parallel and on the opposite side of the plates from each other. The hot fluid header that passes through the gasketed plate heat exchanger is located in the top. This arrangement accounts for the pressure drop and turbulent flow as fluid drops over the plates and into the collection header. Cold fluid enters the bottom of the gasketed plate heat exchanger and travels countercurrent to the hot fluid. The cold fluid collection header is located in the upper section of the exchanger.Plate-and-frame heat exchangers have several advantages and disadvantages. They are easy to disassemble and clean and distribute heat evenly so there are no hot spots. Plates can easily be added or removed. Other advantages of plate-and-frame heat exchangers are their low fluid resistance time, low fouling, and high heat transfer coefficient. In addition, if gaskets leak, they leak to the outside, and gaskets are easy to replace.The plates prevent cross-contamination of products. Plate-and-frame heat exchangers provide high turbulence and a large pressure drop and are small compared with shell-and-tube heat exchangers.Disadvantages of plate-and-frame heat exchangers are that they have high-pressure and high-temperature limitations. Gaskets are easily damaged and may not be compatible with process fluids.Spiral Heat ExchangersSpiral heat exchangers are characterized by a compact concentric design that generates high fluid turbulence in the process medium (Figure 7.22). This type of heat exchanger comes in two basic types: (1) spiral flow on both sides and (2) spiral flow–crossflow. Type 1 spiral exchangers are used in liquid-liquid, condenser, and gas cooler service. Fluid flow into the exchanger is designed for full counterflow operation. The horizontal axial installation provides excellent self-cleaning of suspended solids.Type 2 spiral heat exchangers are designed for use as condensers, gas coolers, heaters, and reboilers. The vertical installation makes it an excellent choice for combining high liquid velocity and low pressure drop on the vapor-mixture side. Type 2 spirals can be used in liquid-liquid systems where high flow rates on one side are offset by low flow rates on the other.Air-Cooled Heat ExchangersA different approach to heat transfer occurs in the fin fan or air-cooled heat exchanger. Air-cooled heat exchangers provide a structured matrix of plain or finned tubes connected to an inlet and return header (Figure 7.23). Air is used as the outside medium to transfer heat away from the tubes. Fans are used in a variety of arrangements to apply forced convection for heattransfer coefficients. Fans can be mounted above or below the tubes in forced-draft or induced-draft arrangements. Tubes can be installed vertically or horizontally.The headers on an air-cooled heat exchanger can be classified as cast box, welded box, cover plate, or manifold. Cast box and welded box types have plugs on the end plate for each tube. This design provides access for cleaning individual tubes, plugging them if a leak is found, and rerolling to tighten tube joints. Cover plate designs provide easy access to all of the tubes. A gasket is used between the cover plate and head. The manifold type is designed for high-pressure applications.Mechanical fans use a variety of drivers. Common drivers found in service with air-cooled heat exchangers include electric motor and reduction gears, steam turbine or gas engine, belt drives, and hydraulic motors. The fan blades are composed of aluminum or plastic. Aluminum blades are d esigned to operate in temperatures up to 300°F (148.88°C), whereas plastic blades are limited to air temperatures between 160°F and 180°F(71.11°C, 82.22°C).Air-cooled heat exchangers can be found in service on air compressors, in recirculation systems, and in condensing operations. This type of heat transfer device provides a 40°F (4.44°C) temperature differential between the ambient air and the exiting process fluid.Air-cooled heat exchangers have none of the problems associated with water such as fouling or corrosion. They are simple to construct and cheaper to maintain than water-cooled exchangers. They have low operating costs and superior high temperature removal (above 200°F or 93.33°C). Their disadvantages are that they are limited to liquid or condensing service and have a high outlet fluid temperature and high initial cost of equipment. In addition, they are susceptible to fire or explosion in cases of loss of containment.。
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换热器外文翻译 (2)
Heat ExchangersKey Terms Baffles—evenly spaced partitions in a shell and tube heat exchanger that support the tubes, prevent vibration, control fluid velocity and direction, increase turbulent flow, and reduce hot spots. Channel head—a device mounted on the inlet side of a shell-and-tube heat exchanger that is used to channel tube-side flow in a multipass heat exchanger.Condenser—a shell-and-tube heat exchanger used to cool and condense hot vapors.Conduction—the means of heat transfer through a solid, nonporous material resulting from molecular vibration. Conduction can also occur between closely packed molecules.Convection—the means of heat transfer in fluids resulting from currents. Counterflow—refers to the movement of two flow streams in opposite directions; also called countercurrent flow.Crossflow—refers to the movement of two flow streams perpendicular to each other.Differential pressure—the difference between inlet and outlet pressures; represented as ΔP, or delta p.Differential temperature—the difference between inlet and outlet temperature; represented as ΔT, or delta t.Fixed head—a term applied to a shell-and-tube heat exchanger that has the tube sheet firmly attached to the shell.Floating head—a term applied to a tube sheet on a heat exchanger that is not firmly attached to the shell on the return head and is designed to expand (float) inside the shell as temperature rises. Fouling—buildup on the internal surfaces of devices such as cooling towers and heat exchangers, resulting in reduced heat transfer and plugging.Kettle reboiler—a shell-and-tube heat exchanger with a vapor disengaging cavity, used to supply heat for separation of lighter and heavier components in a distillation system and to maintain heat balance. Laminar flow—streamline flow that is more or less unbroken; layers of liquid flowing in a parallel path.Multipass heat exchanger—a type of shell-and-tube heat exchanger that channels the tubeside flow across the tube bundle (heating source) more than once.Parallel flow—refers to the movement of two flow streams in the same direction; for example, tube-side flow and shell-side flow in a heat exchanger; also called concurrent.Radiant heat transfer—conveyance of heat by electromagnetic waves from a source to receivers.Reboiler—a heat exchanger used to add heat to a liquid that was onceboiling until the liquid boils again.Sensible heat—heat that can be measured or sensed by a change in temperature.Shell-and-tube heat exchanger—a heat exchanger that has a cylindrical shell surrounding a tube bundle.Shell side—refers to flow around the outside of the tubes of ashell-and-tube heat exchanger. See also Tube side.Thermosyphon reboiler—a type of heat exchanger that generates natural circulation as a static liquid is heated to its boiling point.Tube sheet—a flat plate to which the ends of the tubes in a heat exchanger are fixed by rolling, welding, or both.Tube side—refers to flow through the tubes of a shell-and-tube heat exchanger; see Shell side.Turbulent flow—random movement or mixing in swirls and eddies of a fluid. Types of Heat Exchangers换热器的类型Heat transfer is an important function of many industrial processes. Heat exchangers are widely used to transfer heat from one process to another.A heat exchanger allows a hot fluid to transfer heat energy to a cooler fluid through conduction and convection. A heat exchanger provides heating or cooling to a process. A wide array of heat exchangers has been designed and manufactured for use in the chemical processing industry. In pipe coil exchangers, pipe coils are submerged in water or sprayed with water to transfer heat. This type of operation has a low heat transfer coefficient and requires a lot of space. It is best suited for condensing vapors with low heat loads.The double-pipe heat exchanger incorporates a tube-within-a-tube design. It can be found with plain or externally finned tubes. Double-pipe heat exchangers are typically used in series-flow operations in high-pressure applications up to 500 psig shell side and 5,000 psig tube side.A shell-and-tube heat exchanger has a cylindrical shell that surrounds a tube bundle. Fluid flow through the exchanger is referred to as tubeside flow or shell-side flow. A series of baffles support the tubes, direct fluid flow, increase velocity, decrease tube vibration, protect tubing, and create pressure drops.Shell-and-tube heat exchangers can be classified as fixed head, single pass; fixed head, multipass; floating head, multipass; or U-tube.On a fixed head heat exchanger (Figure 7.1), tube sheets are attached to the shell. Fixed head heat exchangers are designed to handle temperature differentials up to 200°F (93.33°C). Thermal expansion prevents a fixed head heat exchanger from exceeding this differential temperature. It is best suited for condenser or heater operations.Floating head heat exchangers are designed for high temperature differentia is above 200°F (93.33°C).During operation, one tube sheet is fixed and the other “floats” inside the shell.The floatingend is not attached to the shell and is free toexpand.Figure 7.1 Fixed Head Heat ExchangerReboilers are heat exchangers that are used to add heat to a liquid that was once boiling until the liquid boils again. Types commonly used in industry are kettle reboilers and thermosyphon reboilers.Plate-and-frame heat exchangers are composed of thin, alternating metal plates that are designed for hot and cold service. Each plate has an outer gasket that seals each compartment. Plate-and-frame heat exchangers have a cold and hot fluid inlet and outlet. Cold and hot fluid headers are formed inside the plate pack, allowing access from every other plate on the hot and cold sides. This device is best suited for viscous or corrosive fluid slurries. It provides excellent high heat transfer. Plate-and-frame heat exchangers are compact and easy to clean. Operating limits of 350 to 500°F (176.66°C to 260°C) are designed to protect the internal gasket. Because of the design specification, plate-and-frame heat exchangers are not suited for boiling and condensing. Most industrial processes use this design in liquid-liquid service.Air-cooled heat exchangers do not require the use of a shell in operation. Process tubes are connected to an inlet and a return header box. The tubes can be finned or plain. A fan is used to push or pull outside air over the exposed tubes. Air-cooled heat exchangers are primarily used in condensing operations where a high level of heat transfer is required.Spiral heat exchangers are characterized by a compact concentric design that generates high fluid turbulence in the process medium. As do otherexchangers, the spiral heat exchanger has cold-medium inlet and outlet and a hot-medium inlet and outlet. Internal surface area provides the conductive transfer element. Spiral heat exchangers have two internal chambers.The Tubular Exchanger Manufacturers Association (TEMA) classifies heat exchangers by a variety of design specifications including American Society of Mechanical Engineers (ASME) construction code, tolerances, and mechanical design:●Class B, Designed for general-purpose operation (economy and compactdesign)●Class C. Designed for moderate service and general-purpose operation(economy and compact design)●Class R. Designed for severe conditions (safety and durability) Heat Transfer and Fluid FlowThe methods of heat transfer are conduction, convection, and radiant heat transfer (Figure 7.2). In the petrochemical, refinery, and laboratory environments, these methods need to be understood well. A combination of conduction and convection heat transfer processes can be found in all heat exchangers. The best conditions for heat transfer are large temperature differences between the products being heated and cooled (the higher the temperature difference, the greater the heat transfer), high heating or coolant flow rates, and a large cross-sectional area of the exchanger.ConductionHeat energy is transferred through solid objects such as tubes, heads,baffles, plates, fins, and shell, by conduction. This process occurs when the molecules that make up the solid matrix begin to absorb heat energy from a hotter source. Since the molecules are in a fixed matrix and cannot move, they begin to vibrate and, in so doing, transfer the energy from the hot side to the cooler side.ConvectionConvection occurs in fluids when warmer molecules move toward cooler molecules. The movement of the molecules sets up currents in the fluid that redistribute heat energy. This process will continue until the energy is distributed equally. In a heat exchanger, this process occurs in the moving fluid media as they pass by each other in the exchanger. Baffle arrangements and flow direction will determine how this convective process will occur in the various sections of the exchanger.Radiant Heat TransferThe best example of radiant heat is the sun’s warming of the earth. The sun’s heat is conveyed by electromagnetic waves. Radiant heat transfer is a line-of-sight process, so the position of the source and that of the receiver are important. Radiant heat transfer is not used in a heat exchanger.Laminar and Turbulent FlowTwo major classifications of fluid flow are laminar and turbulent (Figure 7.3). Laminar—or streamline—flow moves through a system in thin cylindrical layers of liquid flowing in parallel fashion. This type of flow will have little if any turbulence (swirling or eddying) in it. Laminar flow usually exists atlow flow rates. As flow rates increase, the laminar flow pattern changes into a turbulent flow pattern. Turbulent flow is the random movement or mixing of fluids. Once the turbulent flow is initiated, molecular activity speeds up until the fluid is uniformly turbulent.Turbulent flow allows molecules of fluid to mix and absorb heat more readily than does laminar flow. Laminar flow promotes the development of static film, which acts as an insulator. Turbulent flow decreases the thickness of static film, increasing the rate of heat transfer. Parallel and Series FlowHeat exchangers can be connected in a variety of ways. The two most common are series and parallel (Figure 7.4). In series flow (Figure 7.5), the tube-side flow in a multipass heat exchanger is discharged into the tubeside flow of the second exchanger. This discharge route could be switched to shell side or tube side depending on how the exchanger is in service. The guiding principle is that the flow passes through one exchanger before it goes to another. In parallel flow, the process flow goes through multiple exchangers at the same time.Figure 7.5 Series Flow Heat ExchangersHeat Exchanger EffectivenessThe design of an exchanger usually dictates how effectively it can transfer heat energy. Fouling is one problem that stops an exchanger’s ability to transfer heat. During continual service, heat exchangers do not remain clean. Dirt, scale, and process deposits combine with heat to form restrictions inside an exchanger. These deposits on the walls of the exchanger resist the flow that tends to remove heat and stop heat conduction by i nsulating the inner walls. An exchanger’s fouling resistance depends on the type of fluid being handled, the amount and type of suspended solids in the system, the exchanger’s susceptibility to thermal decomposition, and the velocity and temperature of the fluid stream. Fouling can be reduced by increasing fluid velocity and lowering the temperature. Fouling is often tracked and identified usingcheck-lists that collect tube inlet and outlet pressures, and shell inlet and outlet pressures. This data can be used to calculate the pressure differential or Δp. Differential pressure is the difference between inlet and outlet pressures; represented as ΔP, or delta p. Corrosion and erosion are other problems found in exchangers. Chemical products, heat, fluid flow, and time tend to wear down the inner components of an exchanger. Chemical inhibitors are added to avoid corrosion and fouling. These inhibitors are designed to minimize corrosion, algae growth, and mineral deposits.Double-Pipe Heat ExchangerA simple design for heat transfer is found in a double-pipe heat exchanger.A double-pipe exchanger has a pipe inside a pipe (Figure 7.6). The outside pipe provides the shell, and the inner pipe provides the tube. The warm and cool fluids can run in the same direction (parallel flow) or in opposite directions (counterflow or countercurrent).Flow direction is usually countercurrent because it is more efficient. This efficiency comes from the turbulent, against-the-grain, stripping effect of the opposing currents. Even though the two liquid streams never come into physical contact with each other, the two heat energy streams (cold and hot) do encounter each other. Energy-laced, convective currents mix within each pipe, distributing the heat.In a parallel flow exchanger, the exit temperature of one fluid can only approach the exit temperature of the other fluid. In a countercurrent flowexchanger, the exit temperature of one fluid can approach the inlet temperature of the other fluid. Less heat will be transferred in a parallel flow exchanger because of this reduction in temperature difference. Static films produced against the piping limit heat transfer by acting like insulating barriers.The liquid close to the pipe is hot, and the liquid farthest away from the pipe is cooler. Any type of turbulent effect would tend to break up the static film and transfer heat energy by swirling it around the chamber. Parallel flow is not conducive to the creation of turbulent eddies. One of the system limitations of double-pipe heat exchangers is the flow rate they can handle. Typically, flow rates are very low in a double-pipe heat exchanger, and low flow rates are conducive to laminar flow. Hairpin Heat ExchangersThe chemical processing industry commonly uses hairpin heat exchangers (Figure 7.7). Hairpin exchangers use two basic modes: double-pipe and multipipe design. Hairpins are typically rated at 500 psig shell side and 5,000 psig tube side. The exchanger takes its name from its unusual hairpin shape. The double-pipe design consists of a pipe within a pipe. Fins can be added to the internal tube’s external wall to increase heat transfer. The multipipe hairpin resembles a typical shell-and-tube heat exchanger, stretched and bent into a hairpin.The hairpin design has several advantages and disadvantages. Among its advantages are its excellent capacity for thermal expansion because of its U-tube type shape; its finned design, which works well with fluids that have a low heat transfer coefficient; and its high pressure on the tube side. In addition, it is easy to install and clean; its modular design makes it easy to add new sections; and replacement parts are inexpensive and always in supply. Among its disadvantages are the facts that it is not as cost effective as most shell-and-tube exchangers and it requires special gaskets.Shell-and-Tube Heat ExchangersThe shell-and-tube heat exchanger is the most common style found inindustry. Shell-and-tube heat exchangers are designed to handle high flow rates in continuous operations. Tube arrangement can vary, depending on the process and the amount of heat transfer required. As the tube-side flow enters the exchanger—or “head”—flow is directed into tubes that run parallel to each other. These tubes run through a shell that has a fluid passing through it. Heat energy is transferred through the tube wall into the cooler fluid. Heat transfer occurs primarily through conduction (first) and convection (second). Figure 7.8 shows a fixed head,single-pass heat exchanger.Fluid flow into and out of the heat exchanger is designed for specific liquid–vapor services. Liquids move from the bottom of the device to the top to remove or reduce trapped vapor in the system. Gases move from top to bottom to remove trapped or accumulated liquids. This standard applies to both tube-side and shell-side flow.Plate-and-Frame Heat ExchangersPlate-and-frame heat exchangers are high heat transfer and high pressure drop devices. They consist of a series of gasketed plates, sandwiched together by two end plates and compression bolts (Figures 7.20 and 7.21). The channels between the plates are designed to create pressure drop and turbulent flow so high heat transfer coefficients can be achieved.The openings on the plate exchanger are located typically on one of the fixed-end covers.As hot fluid enters the hot inlet port on the fixed-end cover, it is directed into alternating plate sections by a common discharge header. The header runs the entire length of the upper plates. As cold fluid enters the countercurrent cold inlet port on the fixed-end cover, it is directed into alternating plate sections. Cold fluid moves up the plates while hot fluid drops down across the plates. The thin plates separate the hot and cold liquids, preventing leakage. Fluid flow passes across the plates one time before entering the collection header. The plates are designed with an alternating series of chambers. Heat energy is transferred through the walls of the plates by conduction and into the liquid by convection. The hot and cold inlet lines run the entire length of the plate heater and function like a distribution header. The hot and cold collection headers run parallel and on the opposite side of the plates from each other. The hot fluid header that passes through the gasketed plate heat exchanger is located in the top. This arrangement accounts for the pressure drop and turbulent flow as fluid drops over the plates and into the collection header. Cold fluid enters the bottom of the gasketed plate heat exchanger and travels countercurrent to the hot fluid. The cold fluid collection header is located in the upper section of the exchanger.Plate-and-frame heat exchangers have several advantages and disadvantages. They are easy to disassemble and clean and distribute heat evenly so there are no hot spots. Plates can easily be added or removed. Other advantages of plate-and-frame heat exchangers are their low fluid resistance time, low fouling, and high heat transfer coefficient. In addition, if gaskets leak, they leak to the outside, and gaskets are easy to replace.The plates prevent cross-contamination of products. Plate-and-frame heat exchangers provide high turbulence and a large pressure drop and are small compared with shell-and-tube heat exchangers.Disadvantages of plate-and-frame heat exchangers are that they have high-pressure and high-temperature limitations. Gaskets are easily damaged and may not be compatible with process fluids.Spiral Heat ExchangersSpiral heat exchangers are characterized by a compact concentric design that generates high fluid turbulence in the process medium (Figure 7.22). This type of heat exchanger comes in two basic types: (1) spiral flow on both sides and (2) spiral flow–crossflow. Type 1 spiral exchangers are used in liquid-liquid, condenser, and gas cooler service. Fluid flow into the exchanger is designed for full counterflow operation. The horizontal axial installation provides excellent self-cleaning of suspended solids.Type 2 spiral heat exchangers are designed for use as condensers, gas coolers, heaters, and reboilers. The vertical installation makes it an excellent choice for combining high liquid velocity and low pressure drop on the vapor-mixture side. Type 2 spirals can be used in liquid-liquid systems where high flow rates on one side are offset by low flow rates on the other.Air-Cooled Heat ExchangersA different approach to heat transfer occurs in the fin fan or air-cooled heat exchanger. Air-cooled heat exchangers provide a structured matrix of plain or finned tubes connected to an inlet and return header (Figure 7.23). Air is used as the outside medium to transfer heat away from the tubes. Fans are used in a variety of arrangements to apply forced convection for heattransfer coefficients. Fans can be mounted above or below the tubes in forced-draft or induced-draft arrangements. Tubes can be installed vertically or horizontally.The headers on an air-cooled heat exchanger can be classified as cast box, welded box, cover plate, or manifold. Cast box and welded box types have plugs on the end plate for each tube. This design provides access for cleaning individual tubes, plugging them if a leak is found, and rerolling to tighten tube joints. Cover plate designs provide easy access to all of the tubes. A gasket is used between the cover plate and head. The manifold type is designed for high-pressure applications.Mechanical fans use a variety of drivers. Common drivers found in service with air-cooled heat exchangers include electric motor and reduction gears, steam turbine or gas engine, belt drives, and hydraulic motors. The fan blades are composed of aluminum or plastic. Aluminum blades are d esigned to operate in temperatures up to 300°F (148.88°C), whereas plastic blades are limited to air temperatures between 160°F and 180°F(71.11°C, 82.22°C).Air-cooled heat exchangers can be found in service on air compressors, in recirculation systems, and in condensing operations. This type of heat transfer device provides a 40°F (4.44°C) temperature differential between the ambient air and the exiting process fluid.Air-cooled heat exchangers have none of the problems associated with water such as fouling or corrosion. They are simple to construct and cheaper to maintain than water-cooled exchangers. They have low operating costs and superior high temperature removal (above 200°F or 93.33°C). Their disadvantages are that they are limited to liquid or condensing service and have a high outlet fluid temperature and high initial cost of equipment. In addition, they are susceptible to fire or explosion in cases of loss of containment.。
浮头式列管换热器
目录一、设计方案简介 (3)1.1换热器的概述 (3)1.1.1换热器的分类 (3)1.2列管式换热器的概述 (3)1.2.1列管式换热器的分类 (3)1.2.1.1固定管板式换热器 (3)1.2.1.2浮头式换热器 (4)1.2.1.3填料函式换热器 (5)1.2.1.4U型管式换热器 (5)1.3换热器类型的选择 (5)1.3.1流径的选择 (5)1.3.2流速的选择 (6)1.3.3材质的选择 (7)1.3.4管程结构 (7)二、工艺流程简图 (7)三、工艺计算及主体设备设计 (8)3.1试算并初选换热器规格 (8)3.1.1确定流体通入空间 (8)3.1.2确定流体的定性温度、物性数据,并选择列管换热器的形式 (8)3.1.3计算热负荷Q (9)3.1.4计算平均温差,并确定壳程数 (9)3.1.5初选换热器规格 (9)3.2核算总传热系数K0 (10)3.2.1计算管程对流换热系数 (10)3.2.2计算壳程对流换热系数 (11)3.2.3确定污垢热阻 (11)3.2.4总传热系数 (12)3.3 计算压强降 (12)3.3.1 计算管程压强降 (12)3.3.2 计算壳程压强降 (13)3.4校核壁温 (14)四、换热器主要结构尺寸和计算结果 (14)五、设计感悟 (15)六、参考文献 (16)七、符号说明 (16)附图:工艺流程图以及设备主体图1.设计方案简介1.1换热器的概述换热器(英语翻译:heat exchanger),是将热流体的部分热量传递给冷流体的设备,又称热交换器。
换热器是化工、石油、动力、食品及其它许多工业部门的通用设备,在生产中占有重要地位。
1.1.1换热器的分类按用途它可分为加热器、冷却器、冷凝器、蒸发器和再沸器等。
根据冷、热流体热量交换的原理和方式可分为三大类:间壁式换热器、直接接触式换热器、蓄热式换热器。
间壁式换热器又称表面式换热器或间接式换热器。
在这类换热器中,冷、热流体被固体壁面隔开,互不接触,热量从热流体穿过壁面传给冷流体。
浮头式换热器设计文献综述
浮头式换热器设计文献综述摘要在工业生产中,凡用来实现冷热流体热量交换的设备,统称为换热器。
它在化工、炼油、原子能、建筑、机械、交通等许多技术领域中均有广泛的应用。
如化工生产中的加热器、冷却器、蒸发器、冷凝器、再沸器等;又如热力发电厂中的空气预热器、蒸汽过热器、凝汽器和冷水塔等,为了满足不同生产条件的需要,各工业部门采用多种多样的换热器。
浮头式换热器是石油化工行业广泛使用的热交换设备,其质量的好坏直接影响到石油化工企业的安全和经济效益。
换热器是重要的化工单元操作设备,浮头式换热器是换热器的一种重要类型。
关键词换热器浮头式设计换热器的分类由传热学理论可知道,热交换是一种复杂的过程,它是由系统内两部分的温度差异而引起的,热量总是自动地从温度较高的部分传给温度较低的部分。
传热的基本方式有热传导、对流和辐射3种,因此在换热器中,热量总是从热流体传给冷流体,起加热作用的热流体又称加热介质如水蒸汽、烟道气、导热油或其他高温流体等;起冷却作用的冷流体又称冷却介质如空气、冷冻水、冷冻盐水等。
在热交换过程中,热冷流体的温度是因整个流程而不断变化的,即热流体的温度由于放热而下降,冷流体的温度由于吸热而上升。
适应于各种换热条件,换热器有多种形式。
每种结构形式都有其特点和适用范围,只有熟悉和掌握这些特点,并根据生产工艺具体情况,才能进行合理选型和正确的设计。
适用于不同介质、不同工况、不同温度、不同压力的换热器,结构类型也不同,换热器的具体分类如下:一、换热器按传热原理分类1、表面式换热器表面式换热器是温度不同的两种流体在壁面分开的空间里流动,通过壁面的导热和流体在壁表面对流,两种流体在之间进行换热。
表面式换热器有管壳式、套管式和其他形式的换热器。
2、蓄热式换热器蓄热式换热器通过固体物质构成的蓄热体,把热量从高温流体传递给低温流体,热介质先通过固体物质达到一定温度后,冷介质再通过固体物质被加热,使之达到热量传递的目的。
蓄热式换热器有旋转式、阀门切换式等。
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自由对流热转移反应从垂直加热板到地表热通量的振荡马侯赛因和SK达斯,孟加拉国达卡和DAS里斯,英国巴斯(收稿,1996年6月3日~1996年7月12日修订)总结进行调查的二维不稳定层流沿半无限的竖直板和对流边界的粘性不可压缩流体的层流平均地表热通量关于稳定姿态的小幅度振荡。
浮力是有利的,从积极的热通量板表面的流体与往常边界层流的时间周期热通量的相互作用满足审查线性理论。
解决方案是利用三种不同的方法,即扩展的一系列扩大低频,高频渐近级数展开法和一般频率的数值有限差分法已经进行了广泛的参数计算,以便找到在波动的幅度和相位角的解决方案。
人们已经发现,振幅和相位角,零件表面的剪切应力和表面温度,这三种方法的预测是非常好的在各自有效期的范围。
11介绍在层流边界层理论的领域,莱特希尔[1]是第一个研究的不稳定平板和圆柱与被迫流动的粘性不可压缩流体的自由流,有小幅度的振荡。
自由对流的相似性解决方案从表面均匀热通量与垂直板最初量是研究麻雀格雷格[2]和获得附近的领先优势有效的解决方案。
相应的问题是非定常对流沿垂直板表面温度振荡由纳达和夏尔马[3]和Eshghy等研究。
[4]。
muhuri和梅蒂[5]和Verma[6]分析了非定常自由对流的振荡表面温度的影响。
所有这些调查是基于这样的假设,表面温度执行与时间有关的小振幅振荡意味着温度,和他们进行了通过采用卡门Pohlhausen 近似的积分法。
为了获得有效的领先优势,在附近的摄动解下游地区,罗伊[7]认为是高普朗特数的同类型的问题,威尔克斯[8]研究了一个统一的表面热通量垂直板自由对流的问题。
在规定的地表热通量的垂直板的情况下,研究由梅尔金和Mahmood[,乔杜里和梅尔金[11]等人。
这些作品被源源不断局限,使解决方案得到了有效的距离,解决方案也给出了中间区域。
基于对线性化理论,凯莱赫和杨[12]研究了层流换热反应逃离对流边界层沿垂直加热板表面温度振荡的问题,最近,侯赛因等调查同类型的问题,详细的表面平均温度,θω(x),“其中x与该板块的领先优势的流向距离成正比。
侯赛因等人提出解决方案,在表面热的幅度和相位ζ,流向分布频为小型和大型值的传输速率振荡。
也有人试图匹配低或高频率的振荡。
在相应情况下的自由对流层边界的垂直加热板与非均匀表面热通量还没有被处理之前,应当指出,由于非均匀表面热通量变化可能会出现比物理的表面均匀热通量变化大。
重要的是,要确定具体在多大程度上非均匀表面热通量会影响边界层的响应。
目前本文考虑的粘性不可压缩流体的非定常自由对流沿垂直的加热板时,板面的热通量有小幅度的振荡大于平均通量,它本身作为前沿的距离n的功率变化。
我们调查一般采用(一)延长系列扩展方法低频率范围内,(二)渐近级数展开法在高频率范围,(三)有限差分方法来寻找解决方案的方法。
广泛的进行计算参数,以确定表面上的温度和剪切应力的不稳定的影响。
2数学公式在直角坐标系中,一个半无限的垂直板被放置在y = 0,X_>0的区域,使x的测量距离从前沿进入到流体,而且y的正常测量从进液板进入到流体。
远离表面的环境流体温度为Too。
作为一个积极的表面热通量q~,,,结果从板中产生有利的浮力。
在Boussinesq近似理论下,通常的Navier-Stokes方程和能量方程,两三维不可压缩流体,表面热流率是时间相关的情况下,减少到以下边界层方程(Kramer和排[14]):其中u,v分别为x和速度场y的组件,ν是运动学粘度,T和Too是流体边界层温度和周围流体的温度,g是重力加速度,fl是体积膨胀系数,α是热扩散系数。
方程(1)- (3)要解决的边界条件传热反应103其中ω是振荡频率的表面热通量而是一个衡量它的幅度。
边界条件(4)建议式的解决方案。
(1)- (3)可以发现,作为下列表达式的实部(石垣岛)[15]:其中的组成部分和平均流量基本稳定,满足微分方程边界条件u l, vi和是非定常流的组成部分,它满足的微分方程受边界条件为了获得相似稳定状态方程(6)- (8),我们将介绍以下组的转换:104 文学硕士侯赛因等。
在上面的满足稳态流的连续性方程,而是一个平均地表热通量有关的常数。
因此,我们获得了方程满足上述方程的边界条件是这里的素数用表示,是普朗特数转换(14)带领我们转换以下方程组。
(10)- (13)波动问题的一部分:方程(11)和(12),然后降低到边界条件不稳定的剪应力和表面温度是很难发现的,而这些可以从方程式中得到解决。
(15)- (17)和(19)- (21)。
在这里,我们提出了在振幅和相位的剪应力和表面热流率的解决方案。
根据这些定义和代表的实部和虚部和的一部分。
传热反应方程(15)- (17)描述了稳定的平均流量和温度场。
这些方程的解决方案已经得到乔杜里和梅尔金的[11]相关的物理参数pr和n的不同的价值。
方程(19)- (21)描述的波动的解决方案组成部分,这些应通过多种方法解决。
在第3节我们详细介绍ζ值,使用了一系列解决方案。
由于ζ和ω﹑成正比,见(18),这样的系列解决方案是有效的x小的值而并且为了非常低的频率与。
第4节讨论ζ的渐近解,这可以作为一个大的距离限制,或解释为高频率的限制。
解决方案为中间值ζ。
方程在一般情况下,类似的使用了凯勒盒的方法(见[17])。
实施这种方法的详情,现在非常标准,并已在[13]讨论。
值得注意的是,当n =1的时候。
(19)和(20)降低到一对线性常微分方程的解决方案可以通过一个简单的拍摄方法得到的。
3 的系列解决方案显然,附近的领先优势,使得在使用结果的基础上,数量有限的影响,忽快忽慢的描述将只在很小的范围内有效。
由于ζ小值也对应非常低的频率,ω,我们期望的流量调整准静态传热边界的波动率。
我们扩大f和θ,根据代入式(19)- (20),然后等同为像到零的力量,我们得到以下对函数“”常微分方程:其中M = 1,2,3,各自的边界条件是......素数再次到的衍生物。
106 文学硕士侯赛因等。
可以看出公式(25)- (28)是线性的,但加上可独立解决的从一个到另一个。
在目前的分析,龙格- 库塔- 布彻[18]的初始值问题求解连同Nachtsheim Swigert[19]迭代方案解决式的系统。
(25)- (28)为。
这里的帕德[20]也被用来获得更准确地接近了当地的幅度和相位的剪应力和表面热流的波动部分。
在第5节对详细的数值结果进行了讨论。
4大型的渐近解远离前沿浮力变得越来越重要,直到远离下游的流量将是主要的自由对流,自由流的存在只是略有不安。
因此,在本节已经给予了解决方案。
(19)和(20)ζ当大的时候,我们强调的是,这个限制对应的不仅是为ω定义的x的大值,还有为x定义的ω的大值。
其实,其实,详细检查了凯勒的箱法得到的数值结果显示,ζ的大值,不稳定的反应,只限于表面附近的薄区域。
我们注意到,然而,这个结论没有在更高的电子订单中。
因此,我们寻求在高频率范围内的一系列解决方案中,采用零近似的解决方案。
出于这个原因,介绍了以下转换:这些换算比例的动机顺序数量级分析(19)。
然后成为方程(19)和(20)和由于这些方程对应的是薄壁层,领先高阶函数的,F和,在这个区域可以表示以下功率具有良好的准确性:传热响应107其中,根据公式。
(15)- (17)基于上述展开式的解决方案。
(31)和(32)可以得到以下形式:当公式(35)代入(31)和(32)ζ被收集,包括:和质数现在表示关于差异为Y相关的边界条件现在解决公式(36)和(37),受边界条件(38),我们发现在下面的表达式为和108 文学硕士侯赛因等。
其中我被评为在第一象限(即),并且这里必须指出的是复杂的表达式(39)和(40)是有效的普朗特数,然而,当是需要的,有时必须采取这些解决方案的限制,为。
5结果和讨论在目前的分析,一种粘性波动的自由对流流体的解决方案是使不可压缩流体沿垂直受热面小幅度的在地表热通量非均匀稳定的前沿从测量距离的力量变化的热通量振荡。
(主导的顺序)稳定问题的解决方案已经由乔杜里和梅尔金[11]讨论。
凯勒在整个频率范围内采用箱法分析了波动问题的部分。
该解决方案也已采用渐近法在小频率和大范围的频率使用扰动方法制度。
由此获得的结果表示在幅度和相位、剪应力的波动部分以及那些表面温度呈现出不同的表面热通量梯度参数n和普朗特数的影响方面,普朗特数的值被选择代表目前用于核工程冷却剂为液态金属流体(威尔克斯[8]),例如,锂 0.05 汞0.01。
我们还获得=1.0,0.7,0.1,0.05,0.01的解决方案。
= 1.0和n= 1.0表1和表2给出的剪应力的波动幅度和相位,通过上述三种方法获得的表面温度的数值。
比较结果显示,扰动解和渐近解的差分解决方案很好的吻合。
对于n=0.0,0.25,0.5和0.75 =0.7,对应于空气,这些方法获得的数值,这就是上文所述剪应力波动的幅度和相图图形1和2。
相应的幅度和相位值表面温度波动图所示3和4。
在这些数字的粗曲线。
传热反应109表1。
=1.0剪应力的波动幅度和相和n=1.0a低频率的系列解决方案b 高频率的渐近解代表凯勒盒的解决方案,圆圈和坚实的盘旋曲线代表的扰动解和渐近解。
像以前一样,这些曲线之间的比较确定的扰动解和渐近解与凯勒盒法解决方案在选定的每一个表面热流指数值都非常吻合。
图5 – 6和7 - 8表示剪应力的波动幅度和相位,以及在PR=0.7,0.1,0.05,0.01,N = 0.5的表面温度。
从表1和表2中,我们可以看到随着频率的增加,无论表面温度梯度规定的普朗特数、剪应力幅值和表面传热,单调减少(从图1和3中可以看到)。
这是由于从表面上看,滞后随频率变化量在相邻流体层的温度滞后。
可以看出,在整个频率范围内的表面温度。
110 文学硕士侯赛因等。
表2。
=1.0和n= 1.0表面温度波动的幅度和相位a低频率的系列解决方案b高频率的渐近解振荡总是导致表面温度波动。
相位角,和,在稳态条件下是零,而他们对单调减少渐近值和分别为。
我们进一步观察,在低频率范围内的相位角是随着普朗特数的表面温度梯度减小的值(由此可以看出,从图2和4)。
从图1和3可以看出,在低频范围,剪应力振幅和波动的表面温度降低时指数表面的热通量增加。
同样,从图2和4可以看出,相角在低频率范围内,随着指数增加的价值,而值保持常数。
传热响应111图1剪应力波动的幅度图2针对不同阶段波动的剪力n的值,而=0.7不同的n值,而=0.7图3幅度的波动,表面温度图4。
表面温度波动的相位不同值的n,- =0.7不同的n值,而=0.7图5当n=0.5时,剪应力图6当n=0.5时,针对波动的幅度不同的Pr值不同阶段剪应力的Pr值从图5和7可以看出,在低频范围,随着剪应力和表面温度的振幅,减少而普朗特数增加。