双组分颗粒声场流态化的实验研究

在内径为56 mm的玻璃声场流化床中,以5~10 nm未改性和有机改性的SiO2为实验物料主体颗粒,Fe3O4(粒径小于0.053 mm)为客体颗粒,在声压级为90~105 dB时系统考察了声场频率、声场强度和主客体颗粒不同配比关系对超细颗粒流化行为和聚团尺寸的影响。结果表明,当声场频率处于50 Hz,声压级大于100 dB时,声波可以有效地消除节涌、抑制沟流、降低临界流化速度,减小聚团尺寸,显著改善超细颗粒的流化质量。声场频率一定,声场强度越大,颗粒团聚体的直径越小。客体颗粒的添加比例存在一适宜范围。     

超细颗粒聚团流化的临界流化速度

在内径50 mm的流化床实验台上,测量SiO_2、Al_2O_3和TiO_2 3种超细颗粒原生粒径从30 nm增加到5μm的临界流化速度(Umf),并以Geldart A类颗粒(粒径45μm)为参照。结果表明:3种超细颗粒的Umf随粒径的变化规律一致,随原生粒径从30 nm增加到5μm,Umf逐渐增大;当颗粒粒径增加到45μm,Umf大幅度减小,其与原生粒径为30和200 nm时接近。对于不同材料,Umf由大至小的顺序依次为TiO_2、Al_2O_3、SiO_2。粉体安息角测量表明:对于同种材料颗粒,原生粒径对超细颗粒的Umf和安息角的影响规律一致,即5μm超细颗粒的安息角最大。聚团尺寸模型计算表明:稳定流化时,聚团尺寸随原生粒径的变化趋势以及随不同材料的变化趋势均与Umf的变化趋势一致。研究结果为超细颗粒流化临界速度预测研究奠定了基础。     

超细颗粒流化特性及团聚机理

在直径40mm的流化床中，考察了Al2O3、CaCO3等超细颗粒的流化特性，测定了床层压降变化、床层的坍落及膨胀规律.通过对超细颗粒自团聚现象的分析，探讨了超细颗粒稳定流化的机理.     

超细粉在声场导向管喷流床中的聚团尺寸预测模型

超细粉的流化性能与聚团尺寸密切相关。通过分析超细粉聚团在声场导向管喷流床中的形成过程,提出了高速射流的剪切作用和聚团间的碰撞作用是决定聚团尺寸的主要原因。在此基础上,结合聚团在射流剪切过程和聚团间碰撞过程中的力平衡分析,建立了声场导向管喷流床中聚团尺寸分布的预测模型;并运用这一模型成功预测了不同射流气速下,超细TiO_2颗粒在声场导向管喷流床中的聚团平均直径和聚团尺寸分布。     

超细粉在声场导向管喷流床中的聚团尺寸预测模型

超细粉的流化性能与聚团尺寸密切相关。通过分析超细粉聚团在声场导向管喷流床中的形成过程,提出了高速射流的剪切作用和聚团间的碰撞作用是决定聚团尺寸的主要原因。在此基础上,结合聚团在射流剪切过程和聚团间碰撞过程中的力平衡分析,建立了声场导向管喷流床中聚团尺寸分布的预测模型;并运用这一模型成功预测了不同射流气速下,超细TiO₂颗粒在声场导向管喷流床中的聚团平均直径和聚团尺寸分布。     

超细粉流化机理和团聚现象的探讨

在直径60mm的流化床中，以SiO2和TiO2超细粉为原料，考察了粉体物性、粉体填充状态和空气湿度等因素对超细粉流化行为和聚团性质的影响，结果表明：超细粉的流态化经历了活塞流、过渡区和聚团流化3个阶段；聚团的流化行为与大颗粒相似；初始填充状态对超细粉流化行为和聚团大小有重要影响，松填充有利于减小聚团尺寸和减少颗粒夹带，提高流化质量；并结合粉体层受力分析，对超细粉的流化机理和团聚现象进行了探讨。     

超细颗粒聚团流化的临界流化速度

在内径50 mm的流化床实验台上,测量SiO₂、Al₂O₃和TiO₂ 3种超细颗粒原生粒径从30 nm增加到5 μm的临界流化速度（U_mf）,并以Geldart A类颗粒（粒径45 μm）为参照。结果表明：3种超细颗粒的U_mf随粒径的变化规律一致,随原生粒径从30 nm增加到5 μm,U_mf逐渐增大;当颗粒粒径增加到45 μm,U_mf大幅度减小,其与原生粒径为30和200 nm时接近。对于不同材料,U_mf由大至小的顺序依次为TiO₂、Al₂O₃、SiO₂。粉体安息角测量表明：对于同种材料颗粒,原生粒径对超细颗粒的U_mf和安息角的影响规律一致,即5 μm超细颗粒的安息角最大。聚团尺寸模型计算表明：稳定流化时,聚团尺寸随原生粒径的变化趋势以及随不同材料的变化趋势均与U_mf的变化趋势一致。研究结果为超细颗粒流化临界速度预测研究奠定了基础。     

纳米TiO2颗粒在声场流化床中的流化特性

以原生纳米级TiO2颗粒为物料，在内径为130mm的声场流化床中，考察声压、频率对纳米颗粒的流化特性的影响。结果表明，适当的低频强声波的引入能很好的抑制沟流，消除节涌，大大降低了流化床中纳米颗粒聚团的尺寸，使之在低气速下实现稳定流化，从而显著改善纳米颗粒的流化质量。     

声场流化床中超细颗粒聚团受力与尺寸

在内径40 mm的流化床中,采用平均粒径为7.4 mm的超细铁矿颗粒进行声场流态化实验. 结果显示,聚团尺寸随声压级增大逐渐减小,在固定声压级的条件下存在最优声波频率,本实验为130 Hz. 由铁矿颗粒声场流态化中聚团受力分析提出聚团受力平衡模型,当促进聚团破碎的力和促进聚团形成的力相等时,计算出一定频率不同声压级下的聚团尺寸,在频率130 Hz、声压120.5 db下,根据模型计算得到的聚团直径为384 mm,而通过最小流化速度计算值为367 mm,二者较接近.     

原生纳米级颗粒的聚团散式流态化

在内径为 35mm的小型玻璃流化床中考察了平均原生粒径为 16nm的SiO₂ 颗粒的流化行为 .实验发现 :当操作气速远远超过原生纳米颗粒的最小流化气速时 ,这种超细颗粒可以通过自团聚实现稳定、均匀的散式流化 ,并可获得比GeldartA类颗粒更高的床层膨胀比和更宽的散式操作区 .由于原生纳米级SiO₂ 颗粒在流化时形成的团聚物具有较大的粒径和很小的密度 ,使得该气固体系的流化行为与液固体系有许多相似之处 ,该过程对于研究气固流态化的散式化具有重要意义     

Fluidization characteristics of printed circuit board plastic particles with different sizes

The experiments were carried out in a fluidized bed of 56 mm in diameter and 1 600 mm in height to determine the fluidization characteristics of four sizes of printed circuit board plastic (PCBP) particles. It indicates that the fluidization characteristics of PCBP particles depend on the average size and particle type. 123 µm PCBP particles (1#), belonging to Geldart A group with strong viscous force, whose fluidization behaviours was similar to those of Geldart C, was difficult to fluidize. Whereas, 275 µm (2#), 354 µm (3#), and 423 µm (4#) PCBP particles, belonging to Geldart B, were fluidized smoothly. The bed collapsing process is composed of three stages: the bubble escaping stage, the sedimentation stage, and the solid consolidation stage. The collapsing process of 1# PCBP particle lasts 6 s or long. 2#, 3#, and 4# PCBP particles, Geldart group B particles, collapse process consists of the bubble escaping stage and the solid consolidation stage. The minimum fluidization velocities from modified Ergun Equation were agreement with experimental data for 2#, 3#, and 4# PCBP particles.     

搅拌流化床中超细氧化铁粉流态化及还原实验研究

在内径50 mm的搅拌流化床内进行了平均粒径239 nm的氧化铁粉的流态化及氢气还原实验. 结果表明,床中氧化铁颗粒以聚团鼓泡形式实现完全流化,最小流化速度为0.025 m/s,最大床层膨胀比为2.0. 在500℃下用氢气还原该氧化铁粉的反应过程为：Fe2O3?Fe3O4?Fe,Fe颗粒的粒径比Fe2O3小,有颗粒烧结现象,由Fe引起的颗粒烧结和粘结作用可能导致失流. 与普通流化床相比,搅拌能使流化时间由3 min延长至15 min,使失流时样品的金属化率由15%提高至76%.     

Effect of sound on the fluidization of group B particles

The behaviour of several kinds of group B particles ranging from 100 μm to 600 μm was studied in a sound wave vibrated fluidized bed (SVFB). The fluidized bed consists of a transparent Plexiglas tube that is 54 mm i.d. × 1 m high. A speaker mounted at the top of the bed was supplied by a function generator with square waves and was used to generate the sound as the source of vibration of the fluidized bed. The influence of the particle size, density of particles and sphericity of particles on the minimum fluidization velocity, pressure fluctuations and bubble rise velocity in the SVFB was investigated. The minimum fluidization velocity decreased as the sound energy increased. When the sound energy was strong enough and greater than the critical power, the minimum fluidization velocity would approach the same value regardless of the degree of resonance (DOR) value if the particles were in spherical shape. For non-spherical shape particles the minimum fluidization velocity was the function of the DOR value if the power was greater than the critical power. For the middle particle size range, the standard deviation of pressure fluctuations in an SVFB became lower than the one without the effect of sound in high superficial gas velocity range, but the result was reverse for the low superficial velocity; for the large particle size range, the standard deviation of pressure fluctuations in an SVFB was larger than the one without the effect of sound. The sound could also reduce the bubble rise velocity in an SVFB.     

纳米级SiO2颗粒流化床的塌落行为

在直径为 35mm的小型流化床中考察了纳米级SiO2 颗粒 (商品牌号R972 )的床层塌落行为 .该种经过表面改性的颗粒可以通过自团聚形成稳定、均匀的聚团散式流化 .实验证明 ,这种颗粒的床层塌落行为明显不同于普通的GeldartA类与C类颗粒 ,其塌落过程可分为恒速沉降阶段和减速压实阶段 .通过对塌落速率的分析 ,提出了聚团散式流化的床层塌落机制     

几种典型铁矿粉的流化特性

利用内径150 mm的D型有机玻璃流化床模型,对澳矿、巴西矿、北方矿和钒钛矿典型铁矿粉的流化特性进行了实验研究,获得了其流化特性曲线、初始流化速度和最大床层压降,并将初始流化速度的实测值和理论计算值进行了比较分析. 结果表明,矿粉粒度是影响其流化特性的最主要因素,粒径越大,床层所需要的初始流化速度越大,实测值和理论估算值基本相符;粒度小于0.125 mm钒钛矿流动性较差,在流化过程中易出现沟流现象;粒度范围较宽的矿粉,完全流态化时,细矿粉随气流夹带逸出明显;在粒度相同的情况下,几种不同的铁矿粉的开始流化速度接近,而床层压降有较大差异,巴西矿的床层压降明显大于其他三种铁矿粉. 最大床层压降的最小值均出现在粒度为0.25~0.425 mm,为铁矿粉流态化还原过程中较适宜的粒度范围.     

纳米级SiO2颗粒流化床的塌落行为

在直径为 35mm的小型流化床中考察了纳米级SiO₂ 颗粒 (商品牌号R972 )的床层塌落行为 .该种经过表面改性的颗粒可以通过自团聚形成稳定、均匀的聚团散式流化 .实验证明 ,这种颗粒的床层塌落行为明显不同于普通的GeldartA类与C类颗粒 ,其塌落过程可分为恒速沉降阶段和减速压实阶段 .通过对塌落速率的分析 ,提出了聚团散式流化的床层塌落机制     

Review on the nanoparticle fluidization science and technology

Gas fluidization has an ability to turn static particles to fluid-like dense flow, which allows greatly improved heat transfer among porous powders and highly efficient solid processing to become reality. As the rising star of current scientific research, some nanoparticles can also be fluidized in the form of agglomerates, with sizes ranging from tens to hundreds of microns. Herein, we have reviewed the recent progress on nanomaterial agglomeration and their fluidization behavior, the assisted techniques to enhance the fluidization of nanomaterials, including some mechanical measures, external fields and improved gas injections, as well as their effects on solid fluidization and mixing behaviors. Most of these techniques are effective in breaking large agglomerates and promoting particulate fluidization, meanwhile, the solid mixing is intensified under assisted fluidization. The applications of nanofluidization in nanostructured material production and sustainable chemical industry are further presented. In summary, the fluidization science of multidimensional, multicomponent and multifunctional particles, theirmulti-phase characterization, and the guideline of fluidized bed coupled process are prerequisites for the sustainable development of fluidized bed based materials, energy and chemical industry.     

Model for Calculation of Agglomerate Sizes of Nanoparticles in a Vibro‐fluidized Bed

The behavior of SiO₂ nanoparticles and the effects of operating conditions on nanoparticle agglomerate sizes have been investigated under conditions created in a vibro‐fluidized bed (VFB). The experimental results reveal that the vibrations imposed in the bed can suppress slugging and/or channeling, in contrast to conventional fluidization with upflow only. The vibrations imposed in the particle bed affect both the minimum fluidization velocity and the agglomerate size, both of which decrease with increases in the energy introduced to the bed by the vibrations. The effect of vibrations on the agglomeration in vibro‐fluidized beds of nanoparticles depends on the critical vibration frequency corresponding to a minimum agglomerate size. Both the amplitude and the frequency of the applied vibrations have significant effects on the agglomerate size. The experimental results and the consequent analysis reveal that increasing levels of vibrations in the bed yields finer agglomerates. The Richardson‐Zaki scaling law combined with Stokes law permits the prediction of agglomerate sizes and the extent of initial bed voidage. The average agglomerate sizes predicted are in good agreement with those determined experimentally.