振动流化床中纳米颗粒的流态化行为
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摘要
在传统流化床中考察了黏性纳米SiO_2、ZnO、TiO_2颗粒的流化性能,由于颗粒所特有的物理性质与表面性质,研究发现三种纳米颗粒在低表观气速下易形成活塞和沟流。随表观气速的增加,床内鼓泡加剧,活塞与沟流消失,床中均出现分层现象,扬析严重,流化效果较差。
三种颗粒在振动流化床中均出现平衡压降高于床层重力产生的压降的现象。振动有效地减小了聚团尺寸,提高了床层的气含率,明显改善了流化效果。恒定振幅(3mm)下,振动频率的增加可显著降低纳米颗粒的最小流化速度。与无振动时相比,频率为40Hz时纳米SiO_2的最小流化速度可降低50%;而恒定频率(40Hz)下,振幅的变化对最小流化速度的影响并不是很大。不同高径比下SiO_2物料流态化实验表明,初始颗粒床层高度对颗粒流化性能有较大影响。当床径为一定值(40mm)时,初始床层越高,振动波传播受到的阻碍越大,振动效果越不明显。本实验中,h_o/D=1时,纳米SiO_2的流化效果最好。振动和气速协同作用可以有效地抑制气泡的形成与合并。低气速、高振动频率或高气速、低振动频率都可以获得好的流化效果。与振动频率、振幅和气速相比,流化次数对黏性颗粒的流态化影响相对较微弱,由于在二次流化后形成相对较为稳定的聚团,故颗粒床流化性能基本上不再随流化次数的增加而发生较大改变。
基于Ergun方程和Richardson-Zaki方程定义了两种聚团直径——最小流化速度聚团直径和终端速度聚团直径。通过计算,对黏性纳米聚团的减小进行了证实,并据此对聚团的合并与破碎进行了分析。计算结果与实验值一致。
The behavior of different cohesive nano-particles was investigated in the conventional fluidized bed. It was found that slugs and channels were formed firstly under low superficial gas velocity due to the specific physical and surficial properties of particle. With increasing the superficial gas velocity, slugs and channels vanished, whilst the bubbling in bed was intensified obviously, and there existed a distribution of agglomerate sizes, namely, the agglomerates sizes were small in the upper zone and large in the lower zone. Because of the severe entrainment, the fluidization ability was poor.
Vibrations imposed on gas-fluidized beds of nano-particles caused increase in equilibrium pressure drop, and improved fluidization quality obviously with effectively reduction of agglomerate size as well as looser bed layer. At certain amplitude (3mm) of vibrations applied, the minimum fluidization velocity decreased significantly with increasing vibration frequency. Comparing to the fluidization without vibration, the minimum fluidization velocity of SiO_2 under vibration in this study could be reduced by 50%; while the minimum fluidization velocity was nearly independent of vibration amplitude at almost constant frequency of about 40Hz. Experimental results proved that a proper original bed height of nano-particles with a constant bed diameter (40mm) contributed to better fluidization quality which could be obtained at h_0/D=1 for SiO_2 nano-particles. Further, combinations of high gas velocity and low vibration frequency as well as high vibration frequency and low gas velocity assured two domains with favorable conditions to perform stable fluidization. It could be concluded that the effect of fluidization times on fluidization behavior was relatively small comparing with the other three parameters (vibration frequency, amplitude, gas velocity). The agglomerates sizes were relatively stable after the second fluidization.
Combining the Ergun and the Richardson-Zaki equations, two types of agglomerate size, namely agglomerate size at the minimum fluidization velocity and agglomerate size at the terminal fluidization velocity, have been calculated to confirm the reduction of agglomerate size. The probability of agglomerate coalescence and breakup has beenanalyzed. The calculated values were in agreement with the experimentalresults.
三种颗粒在振动流化床中均出现平衡压降高于床层重力产生的压降的现象。振动有效地减小了聚团尺寸,提高了床层的气含率,明显改善了流化效果。恒定振幅(3mm)下,振动频率的增加可显著降低纳米颗粒的最小流化速度。与无振动时相比,频率为40Hz时纳米SiO_2的最小流化速度可降低50%;而恒定频率(40Hz)下,振幅的变化对最小流化速度的影响并不是很大。不同高径比下SiO_2物料流态化实验表明,初始颗粒床层高度对颗粒流化性能有较大影响。当床径为一定值(40mm)时,初始床层越高,振动波传播受到的阻碍越大,振动效果越不明显。本实验中,h_o/D=1时,纳米SiO_2的流化效果最好。振动和气速协同作用可以有效地抑制气泡的形成与合并。低气速、高振动频率或高气速、低振动频率都可以获得好的流化效果。与振动频率、振幅和气速相比,流化次数对黏性颗粒的流态化影响相对较微弱,由于在二次流化后形成相对较为稳定的聚团,故颗粒床流化性能基本上不再随流化次数的增加而发生较大改变。
基于Ergun方程和Richardson-Zaki方程定义了两种聚团直径——最小流化速度聚团直径和终端速度聚团直径。通过计算,对黏性纳米聚团的减小进行了证实,并据此对聚团的合并与破碎进行了分析。计算结果与实验值一致。
The behavior of different cohesive nano-particles was investigated in the conventional fluidized bed. It was found that slugs and channels were formed firstly under low superficial gas velocity due to the specific physical and surficial properties of particle. With increasing the superficial gas velocity, slugs and channels vanished, whilst the bubbling in bed was intensified obviously, and there existed a distribution of agglomerate sizes, namely, the agglomerates sizes were small in the upper zone and large in the lower zone. Because of the severe entrainment, the fluidization ability was poor.
Vibrations imposed on gas-fluidized beds of nano-particles caused increase in equilibrium pressure drop, and improved fluidization quality obviously with effectively reduction of agglomerate size as well as looser bed layer. At certain amplitude (3mm) of vibrations applied, the minimum fluidization velocity decreased significantly with increasing vibration frequency. Comparing to the fluidization without vibration, the minimum fluidization velocity of SiO_2 under vibration in this study could be reduced by 50%; while the minimum fluidization velocity was nearly independent of vibration amplitude at almost constant frequency of about 40Hz. Experimental results proved that a proper original bed height of nano-particles with a constant bed diameter (40mm) contributed to better fluidization quality which could be obtained at h_0/D=1 for SiO_2 nano-particles. Further, combinations of high gas velocity and low vibration frequency as well as high vibration frequency and low gas velocity assured two domains with favorable conditions to perform stable fluidization. It could be concluded that the effect of fluidization times on fluidization behavior was relatively small comparing with the other three parameters (vibration frequency, amplitude, gas velocity). The agglomerates sizes were relatively stable after the second fluidization.
Combining the Ergun and the Richardson-Zaki equations, two types of agglomerate size, namely agglomerate size at the minimum fluidization velocity and agglomerate size at the terminal fluidization velocity, have been calculated to confirm the reduction of agglomerate size. The probability of agglomerate coalescence and breakup has beenanalyzed. The calculated values were in agreement with the experimentalresults.
引文
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[2]易江林,金涌,俞芷青,等.MSB树脂的流化床干燥.见:第五届全国干燥技术交流会议论文集.上海:1995,316-319
[3]崔玉斌,魏飞,金涌,等.气固逆并流多级旋流干燥的流体力学行为研究.化工冶金,1996,17(3):248-253
[4]黄水源,汪展文,金涌,等.气固循环流化反应器的流体力学行为.化工学报,1996,47(3):357-361
[5]Zhu J X.Personal Communication,University of Western Ontario,1999,London,Ontario,Canada
[6]蔡平,金涌,俞芷青,等.鼓泡流态化向湍动流态化过渡的判别.化工学报,1986,4:341-401
[7]金涌,俞芷青,张礼,等.流化床反应器塔形内构件的研究.化工学报,1980,2:117-127
[8]汪展文,金涌,姚文虎,等.湍动流化床醋酸乙烯合成反应器的工业试验.化学反应工程与工艺,1995,11(1):50-55
[9]杨贵林,黄哲,陈大保,等.快速流化床H-98催化剂丁烯氧化脱氢制丁二烯.石油化工,1988,16(10):680-685
[10]Squires A M.The story of fluid catalytic cracking.Circulating fluidized bed technology,ed.P Basu,Pergamon Press,Toronto,1986,1-19
[11]Bai D R,Zhu J X,Jin Y,et al.Novel designs and simulations of FCC Riser Regenerator.Ind.Eng.Chem.Res,1997,36(11):4543-454
[12]Shingles T,McDonald A F.Commercial experience with synthol CFB reactors.In:P Basu,J F Large,eds.Circulating fluidized bed technology Ⅱ.Pergamon Press,Toronto,1988,43-50
[13]时钧,汪家鼎,余国琮,等.化学工程手册.化学工业出版社,北京:1996
[14]Reh L.The circulating fluid bed reactor-A key to efficient gas/solid Processing.In:P Basu,J F Large,eds.Circulating fluidized bed technology.Pergamon Press,Toronto,1986,105-118
[15]Zhu J X,Bi H T.Distinctions between low density and high density circulating fluidized beds.Journal of Chemical Engineering of Japan,1995,73:644-649
[16]Mawatari Y,Ikegami T,Tatemoto Y,et al.Prediction of Agglomerate Size for Fine Particles in a Vibro-fluidized Bed.Journal of Chemical Engineering of Japan,2003,36(3):277-283
[17]Wilhelm R H,Kwauk M.Fluidization of Solid Particles.Chem.Eng.Progr.,1948,44:201-218
[18]李洪钟,郭慕孙.气固流态化的散式化.化学工业出版社,北京:2002
[19]Doichev,K.Energetic aspects of the transition between aggregative and particulate fluidization.Chem.Eng.Sci.,1974,29:1205-1210
[20]Harrison,D,Davidson J F,De Kock J W.On the nature of aggregative and particulate fluidization.Trans.Inst.Chem.Eng.Sci.,1961,39:202-211
[21]Foscolo P U,Gibilaro L G.A fully predictive criterion for the transition between particulate and aggregative fluidization.Chem.Eng.Sci.,1984,39:1667-1675
[22]Liu D,Kwauk M,Li H Z.Aggregative and particulate fluidization-the two extremes of a continuous spectrum.Chem.Eng.Sci.,1996,51(17):4045-4063
[23]Wen C Y,Yu Y H.A generalized method for predicting the minimum fluidization velocity.AIChE J.,1996,12:610
[24]Geldart D.Types of gas fiuidization.Powder Technology,1973,7:285-292
[25]Geldart D,Harnby N,Wong A C.Fluidization of cohesive powders.Powder Technology,1984,37:25-37
[26]刘得金.超临界流体流态化:[博士学位论文].北京:中国科学院化工冶金研究所,1994
[27]周涛.黏性颗粒聚团流态化实验与理论研究:[博士学位论文].北京:中国科学院化工冶金研究所,1998
[28]Zhou T,Li H Z.Effects of adding different size particles on fluidization of cohesive particles.Powder Technology,1999,102(3):215-220
[29]周涛,李洪钟.黏附性颗粒添加组分流态化实验.化工冶金,1998,19(3):231-236
[30]周涛,李洪钟,王兆霖.粘附性颗粒添加组份流态化进展.化工冶金,1998,19(2):186-192
[31]郭慕孙,翁绍林,王尊孝,等.波纹挡板流态化装置.中国实用新型专利:ZL92207714.2,1993
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