液固流化床换热器分布装置及其分布性能研究
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摘要
本文设计并安装了一套用于换热和防除垢的液固流化床换热器，并运用CCD图象采集与处理系统对分布板的设计进行了实验研究，讨论了分布板结构以及各种操作条件对管束中颗粒的速率、固含率分布的影响。利用Matlab语言实现了实验结果的可视化。实验结果表明：在液固循环流化床进口段安装可调节高度的变孔径分布板，能在较高的流速下，较好的改善固体颗粒在管束中的不均匀分布；开孔率越小固体颗粒在管束中的分布越均匀，但管束中粒子的平均固含率也越小；分布板的安装高度对颗粒的分布有很大的影响，在实验范围内分布板的安装距离管束入口处越远，颗粒在管束中的分布越均匀。所以应根据不同的操作条件选择合适的变孔径分布板，以得到较均匀的粒子分布。根据实验结果建立了固含率与固相速度不均匀度的关联式，并根据颗粒离散模型建立了颗粒速度分布模型，实验结果和计算结果吻合较好。
A solid-liquid fluidized bed has been designed and installed ,which will be used in the heat exchanging and descale field .The experimental study for distributor design was carried out and the particles distribution in the tubes of the solid-liquid fluidized bed under different operating conditions was studied by using the CCD measure system .Experimental results show that heterogeneous pores distributor which was arranged in the inlet chamber of the solid-liquid fluidized bed can improve the nonuniform distribution of particles in the pipe bundle under high flow rate . The nonuniform decreases by decreasing the mount of pore, but the solid holdup decreases too. The particles distribution is influenced by the position of the heterogeneous pores distributor. The nonuniform of distribution decreases with the increase of the distance between distributor and the tubes inlet in operating range. So based on the given operating range, the reasonable pore rate and position of heterogeneous pores distributor can be determined to obtain the distribution of particles as homogeneous as possible. According to the experimental result ,the relevancy formulae were proposed, and according to discrete particle model, particle velocity distribution model was proposed and the experimental result agreed with the calculated result.
A solid-liquid fluidized bed has been designed and installed ,which will be used in the heat exchanging and descale field .The experimental study for distributor design was carried out and the particles distribution in the tubes of the solid-liquid fluidized bed under different operating conditions was studied by using the CCD measure system .Experimental results show that heterogeneous pores distributor which was arranged in the inlet chamber of the solid-liquid fluidized bed can improve the nonuniform distribution of particles in the pipe bundle under high flow rate . The nonuniform decreases by decreasing the mount of pore, but the solid holdup decreases too. The particles distribution is influenced by the position of the heterogeneous pores distributor. The nonuniform of distribution decreases with the increase of the distance between distributor and the tubes inlet in operating range. So based on the given operating range, the reasonable pore rate and position of heterogeneous pores distributor can be determined to obtain the distribution of particles as homogeneous as possible. According to the experimental result ,the relevancy formulae were proposed, and according to discrete particle model, particle velocity distribution model was proposed and the experimental result agreed with the calculated result.
引文
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[2] C.A.Allen et al. Department of energy, Idaho operations offer Under contract,1978,4:1507
[3] T.A.M.merjer.Ph.D. Dissertation. Delft University of Technology,1984
[4] A.W.Veenman.A Review of New Department in Desalination by Distillation Process.Desalination, 1987,(27):21～39
[5] Rautenbach R,Exdmann C, Kollbach J St.. The Fluidized Bed technique in the Evaporation of Wastewater with severe Fouling/Scaling Potential lattes. Development/Application/Limitations. Desalination, 1991,81(3):285～298
[6] Kollbach J St Dahm W ,Rautenbach R .continuous Cleaning of Heat Exchanger with Recirculating Fluidized Bed. Heat Transfer Engineering, 1987,8(4):26～32
[7] Meijer J A M.Prevention of Calcium Suphat Scale Deposition by a Fluidized Bed.Desalination, 1983,47(5):3～15
[8] Klaren D G. Fluidized Bed Heat Transfer Exchanger:A Major Improvement in Severe Fouling Heat Transfer.In:Taborek J. Heat Exchanger:Theory and Practice. Washington: Hemisphere Publishing Corporation, 1981,885～896
[9] Klaren D G, Bailie R E. The Non-fouling Fluidized Bed heat Exchanger.In: Shah R H.National Heat Transfer Conference HTD,Vol. 108:Heat Transfer Equipment Fundamentals Design, Application and Operating Problems.New York:ASME, 1989.273～279
[10] 齐世学，宗详荣，王琳．流化床换热器的研究．[J]烟台大学学报(自然科学与工程版)，1994(1)：48～54
[11] Klaren D G. Apparatus for Carrying out a Physical and/or Chemical Process, Such as Heat Exchanger EP,626550.1994,11～30
[12] 叶施仁．液固流态化换热器结构的改进及应用，[J]化工机械，1998,25(1)：31～33
[14] 郭慕孙，庄一安．流态化—垂直系统中均匀球体和流体的运动．北京：科学出版社，1963，35～53
[15] 刘吉普，吴金香．管程内循环液固流态化强化换热技术研究，[J]湘潭大学自然科学报，1996，18(3)：79～84
[16] 李修伦，刘绍从．汽液固三相流化床沸腾传热的研究，[J]化工学报，1993,44(2)：224～229
[17] 张少峰．三相循环流化床蒸发器防除垢和强化传热的研究，博士学位论文，天津大学研究生院,2000
[18] 吴若琼．防止氧化铝厂蒸发器结垢的新方法，[J]中南工业大学学报，1999,30(1)：45～48
[19] 贾丽云，液固循环流化床和流化床换热器流动特性的研究．[学位论文]，天津大学，1998
[20] Glickman L R, Piper G A .Particle density distribution in the freeboard of a fluidized bed. Powder technology, 1978,53(3):179～283
[21] Choi J H,Yi C K, Son J E.Axiall Voidage. Profile in a cold mode circulating fluidized bed. Circulating Fluidized Bed Technology Ⅲ.Basu P ,ed. oxford: ergamun press, 1990,131～135
[22] 梁五更，张书良，俞芷青等．液固循环流化床的研究(Ⅰ)，[J]化工学报，1993，44(6)：667～671
[23] Wether J ,Hartge D. Measurement techniques for gas-solid fluidized-bed actors. International Chemical Engineering.1993,33(1):18～27
[24] Hartge E U.Dissertation,TU Hamburg-Harbug,1989
[25] Hartge E U, Rensner D , Werther J. Wissenschaftliche forschungasarbeit.Chemic Ingenious technik. 1989,61 (9):744～745
[26] Takeuchi H.,Hirama T .Flow visualization in the riser of a circulating fluidized bed. Circulating Fluidized Bed Technology Ⅲ Basu P ,ed .oxford: Pergamun press, 1990,177～182.
[27] Gbavicic Z B ,Vukovic D V, Zdanski F K. Tracer Particle movement in a two-dimensional water-fluidized bed. Powder Technology, 1990,62:199～201
[28] Chen R C, Fan L S. Particle image velocity meter for characterizing the flow structure in three-dimensional gas-liquid-solid fluidized beds. Chemical Engineering Science, 1992, 47(13/14):3615～3622
[29] 孙国钢，钱贵华，李静海．循环流化床稀相流动局部空隙率的测量．[J]化工冶金，1996，17(3)：242～247
[30] Bukeii J J,Grave J R, Zhao J, et al. Measurement of solid circulating rates in circulating fluidized beds. Circulating Fluidized Bed Technology Ⅱ .Basu P ,ed.Pergamon press,1988,501～509
[31] Boussiness.J.Essay on the Theory of Flow Water Paris,Mem. Acad .sci: 1877(23):1～680
[32] 王树立，张雅琴，张敏卿．湍流两相流动模式理论综述及展望．[J]抚顺石油学院学报，1997，17(2)：37～43
[33] Gosman A D,Ioannides E .AIAA, 198 1:81～323
[34] Boysan F, Ayers W H. Swithenbank. Trans. Inst. Chen. Eng. 1982,60:222
[35] Zhou Lixing. Mixing and Combustion in Two-Phase Flow a Pulverized-Coal Flame Stabilized by a Plasma Jet. 2rid Asian Conger. on Fluid Mech. Beijing china :1983
[36] Ishii M. Thermo-Fluid Dynamic Theory of Two-Phase Flow. Eyrolles Paris :1957
[37] Lahey R T, Drew D A. The Current State -of-art in the Modeling of Vapor Liquid Two-Phase Flow. As ME Reprint, 1990,90-WA/HT-13
[38] 王维，李佑楚．颗粒两相流模型研究进展．[J]化学进展，2000，12(2)：207～217
[39] 刘大有．二相流体动力学．高等教育出版社，北京，1993．30～102
[40] 樊建人，赵华．气固两相流动的湍流脉动扩散数学模型及其应用．[J]应用力学学报，1990，7(1)
50～55
[41] 许国军，王樟茂，陈甘棠．液—固流化床的流体流动和颗粒循环模型．[J]化学反应工程与工艺，1995，11(3)：277～282
[42] 刘大有．现有泥沙理论的不足和改进——扩散模型和费克定律适用性的讨论．[J]泥沙研究，1995(3)：39～45
[43] 刘大有．论气(水)力输送中颗粒悬浮机理和悬浮功。第七届全国化学工程论文报告会文集(上)．北京，1994，251～254
[44] 刘大有，路展民．竖置管流中液固两相脉动特性和颗粒浓度分布．[J]力学学报，2000，32(5)：554～558
[45] 梁五更，张书良，俞芷青，等．液固循环流化床的研究(Ⅱ)表观滑落速度及曳力系数．[J]化工学报，1993，44(6)：672～675
[46] 梁五更，张书良，俞芷青，等．液固循环流化床的研究(Ⅰ)相含率及颗粒循环速率．[J]化工学报，1993，44(6)：666～671
[47] 贾丽云，李修论，刘姝红，等．液固循环流化床两相流动模型．[J]化工学报，2000，51(4)：531～534
[48] 朱靖宇，周昆颍，陈罕．液—固两相流在垂直管束中的稳定性分折．[J]北京化工大学学报，2001，28(2)：64～69
[49] 王维，李佑楚．循环上升管内颗粒团聚行为的动态模拟．[J]化工学报，2000， (51)：84～87
[50] 刘大有．建立两相流方程的动力论方法．[J]力学学报，1987，19(3)
[51] 倪晋仁．王光谦．高浓度恒定固液两相流运动机理探析。[J]水利学报，2000，(5)：22～26
[52] 倪晋仁，王光谦，张红武．[M]固液两相流基本理论及其最新应用．科学出版社，1991
[53] 刘大有．[M]二相流体动力学．高等教育出版社，1993，442～585
[54] 刘大有，吴邦贤，扩散速度与组元的质量守恒方程，[J]应用数学和力学，1991，12(11)
[55] 欧阳洁，李静海．中国科学(B)辑，1999，29(1)：29～38
[56] 徐江荣．多相流颗粒轨道模型的一种新解法．[J]杭州电子工业学院学报，1997，17(3)：16～20
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