纳米SiO2中添加大粒径组分的流化性能

以平均原生粒径为10nm的SiO2为原料，采用添加较大球形玻璃珠颗粒的方法，在内径为60nm的有机玻璃流化床中，考察了在不同添加量和不同添加颗粒粒径的情况下，纳米颗粒SiO2在流化性能。实验表明，纳米颗粒SiO2的流化经历了沟流、节涌破碎和聚团4个阶段，但当添加玻璃珠的量大于10：1或添加玻璃珠粒径不大于0．13mm时，SiO2的流化质量较好，并可采用床层压降曲线来表示其流化性能。     

纳米SiO2对动态硫化EPDM/PP热塑性硫化胶性能的影响

采用不同硫化体系动态硫化制备三元乙丙橡胶/聚丙烯热塑性硫化胶(EPDM/PP TPVs),并在制备的过程添加不同量的纳米SiO2。结果表明酚醛树脂2402动态硫化得到的EPDM/PP TPVs性能最佳。随着纳米SiO2添加量的增加,EPDM橡胶粒子的粒径先减小后增大,当纳米SiO2的添加量为10份时,EPDM橡胶粒子的粒径达到最小。流变性能研究表明添加纳米SiO2使EPDM/PP TPVs的加工性能变差。动态机械分析仪(DMA)研究表明纳米SiO2提高了TPVs中PP相的玻璃化转变温度。当纳米SiO2的添加量为10份,TPVs的拉伸强度达到最高为23.7MPa,提高了19.1%,断裂伸长率达到最大为431%,提高了11.1%。纳米SiO2使EPDM/PP TPVs的热稳定性和耐热老化性能变好。     

纳米SiO2在添加磁性大颗粒磁场流化床中的流态化

研究了纳米SiO2在添加磁性大颗粒磁场流化床中的流化性能,实验中通过测量其床层膨胀曲线、床层压降曲线以及塌落曲线表明:磁性大颗粒在交变磁场下的振动作用可以破碎流化床中纳米SiO2的大聚团.使床层压降和床层膨胀明显增大,流化质量获得显著提高.实验同时考察了磁场强度、磁性颗粒的添加量以及不同的静床高度等参数对流化性能的影响.获得了最佳工艺操作条件.     

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。     

粘附性颗粒添加组份流态化实验

以不同粒径的ＳｉＣ为物料,考察了表观气速和添加颗粒对其流化性能的影响．实验表明,平均粒径大于１０μｍ的ＳｉＣ物料,可通过增大表观气速使其流化;而小于５μｍ的ＳｉＣ５和ＳｉＣ２物料,不能使用增大表观气速的方法使其流化．添加颗粒能使ＳｉＣ５很好流化,利用流态化聚团准数Ａｅｆ可计算颗粒的最佳添加量ｘｍ．     

粒径及声场对SiO2超细颗粒流化行为的影响

采用内径为56 mm的玻璃管流化床,考察了平均粒径分别为5~10 nm(1#), 0.5 mm(2#)及10 mm(3#)的SiO2超细颗粒在无声场及声场存在下的流化行为. 无声场时,1#和2#颗粒可在较高的气速下形成稳定聚团,单位质量颗粒团间作用力与原生颗粒相比显著下降,因而可实现稳定的聚团流化,3#颗粒因颗粒间粘性力较大,无法实现稳定流化. 40~60 Hz的声场对3种超细颗粒的流化行为均可起到一定的改善作用,在此频率范围外,声场的作用不明显. 提高声压级,可以使1#和2#颗粒团发生一定程度的破碎,聚团尺寸减小,最小流化速度降低. 在实验范围内,添加声场无法使3#颗粒实现稳定流化.     

纳米SiO2/丙烯酸UV屏蔽透明涂料的制备及性能研究

通过在丙烯酸树脂中添加不同含量的纳米SiO2，采用共混法制备了纳米SiO2／丙烯酸UV屏蔽透明涂料。研究了纳米SiO2不同添加量时涂料的UV屏蔽性、透明性、粘度及硬度，并对纳米SiO2添加量为3％的涂料样品进行了TEM分析和基本性能测定。     

超细颗粒在声场流化床中的流化特性

在内径为130mm的声场流化床中,以原生纳米级SiO2超细颗粒为物料,在声压水平为0～140dB、声波频率为0～500Hz范围内系统地考察了声波对超细颗粒流化特性的影响。结果表明：当声波频率为100～150Hz、声压大于130dB时,声波可以有效地消除节涌、抑制沟流、降低临界流化速度,显著地改善纳米SiO2颗粒的流化质量。在频率一定的情况下,声压越高,超细颗粒的临界流化速度越低,流化质量越好。当频率低于100Hz或高于150Hz时,随着频率的进一步降低或增加,超细颗粒的临界流化速度都增大,甚至又出现节涌和沟流。声波的效果减弱甚至消失。     

生物质和惰性颗粒二组分混合物的最小流化速度

实验发现纯锯末不能在流化床中流化，锯末中加入惰性固体颗粒构成锯末／玻璃珠、锯末／沙子双组分混合物可实现流化．研究了不同粒径、不同配比混合物的流化规律．已有的预测双组分混合物最小流化速度的公式不能应用于锯末／玻璃珠、锯末／沙子双组分混合物．同时研究了球形、椭圆形菜籽的最小流化速度，并研究了不同粒径菜籽与不同粒径沙子在不同比例下的最小流化速度，结果表明形状规则生物质／惰性颗粒混合物最小流化速度可由Ｃｈｉｂａ公式计算     

聚乙烯亚胺对纳米SiO2空心颗粒分散行为的影响

采用在制备过程中添加聚电解质型分散剂聚乙烯亚胺(PEI)和在制备好的纳米SiO2空心颗粒水悬浮液中添加PEI并球磨这两种方法对纳米SiO2空心颗粒进行分散,并对这两种方法进行了比较,最后采用以PEI作为分散剂,利用球磨工艺,对已制备的纳米SiO2空心颗粒水悬浮液进行分散的方法,研究了PEI在纳米SiO2空心颗粒表面的吸附行为及水悬浮液的分散稳定性.结果表明,PEI在纳米SiO2空心颗粒表面的吸附提高了颗粒间的排斥势能,改善了纳米SiO2空心颗粒的团聚问题及其悬浮液的稳定性.并阐明了加入PEI后纳米SiO2空心颗粒表面ζ电位的变化趋势、不同pH值下PEI在纳米SiO2空心颗粒表面的吸附量与其加入量的关系等.     

Onset of an innovative gasless fluidized bed—comparative study on the fluidization of fine powders in a rotating drum and a traditional fluidized bed

Geldart group C powders were found to be fluidized in rotating drums without requiring any external fluidizing gas. As a result, a rotating drum was proposed as a new gasless fluidized bed in contrast to a traditional fluidized bed, leading to a considerable amount of energy savings. In addition, the fluidization qualities of a series of Geldart group C powders were found to be further improved with the assistance of drum rotation because of the shearing movement among particles that eliminates channeling and cracks and possibly also breaks agglomerates. There is potential for the new gasless fluidized bed to replace some traditional fluidized beds where the fluidizing gas is not used as a reactant.In the gasless fluidized bed, a boundary layer of compacted powder adjacent to the drum wall was observed. The powder in this layer is carried up to the freeboard and then falls back to the powder bed, forming a powder circulation in the drum. The circulating powder leads to a circulation of internal gas in the drum, which essentially acts as fluidizing gas to realize the fluidization of Geldart C powders in the drum. In contrast to the fluidization of Geldart C powders, Geldart groups B and D powders show cascading and cataracting motions instead in the rotating drum due to their requirement of higher fluidization gas velocities. Geldart group A powders experience a transition of powder behavior between Geldart group B–D powders and C powders.     

Floating internals in fast bed of cohesive particles

Four kinds of spherical materials with diameter between 0.3 mm to 0.6 mm were employed as floating internal in fast bed of cohesive particles to reduce agglomerate size and narrow the size distribution. The fast bed of cohesive particles with floating internals preserves basic fluidizing characteristics of fast fluidization. However, the size of agglomerates in fast beds of all four types of cohesive particles employed in experiments was notablely reduced. The effect of floating internals could be obviously observed only when the fluidizing gas velocity is higher than about 3-4 times of incipient fluidizing velocity of floating internals. This phenomenon may indicate an “active velocity” for floating internals to take effect. Under specific operating conditions and a matching between cohesive powder and floating internal, there will be a maximal agglomerate size that floating internals can break. This suggests a proper startup procedure for fast bed with floating internals to prevent the formation of oversize agglomerates. Methods for estimating the gas velocity at which floating internal take effect and the terminal velocity of floating internals and agglomerates were developed to give operating range of fluidizing gas velocity of fast bed with floating internals. A model for calculating maximal agglomerate size that floating internal can break was also developed, and an analysis on the influence of fast bed's operating conditions on the maximal size was made based on the model.     

气固流化床中细长颗粒数量浓度分布的数值研究

细长颗粒的循环流化在工业生产中具有非常广泛的应用背景,如生物质秸秆在循环流化床中的燃烧、烟丝在循环流化床中的干燥或加湿等。由于细长颗粒具有六自由度,因此,其运动姿态比球形颗粒复杂,其在流化床内的流化特性也不同于球形颗粒。细长颗粒的数量浓度分布是细长颗粒流化特性的重要特征之一。根据直接模拟Monte Carlo(DSMC)方法的基本思想及刚体动力学原理,建立了考虑细长颗粒间相互碰撞的三维细长颗粒流化运动数学模型,并采用此模型对某一实际流化床内的气固两相流场进行了模拟研究。在实验提升管内,所有物料中小长径比的细长颗粒最先由提升管的近壁处到达提升管出口。细长颗粒在流化过程中有明显的迁移和絮团现象。在流化状态下,细长颗粒的数量浓度分布基本不随入口风速发生变化。     

磁性纳米Fe3O4在磁场协助作用下的流态化研究

磁性纳米Fe3O4的密度及黏性较大,透气性差,在传统流化床中很难实现“正常”流态化。实验采用外加磁场能的方法来改善这种状况,外加磁场、铁磁性大颗粒并与流化性能较好的非磁性物料混合流化。实验发现在一定磁场强度、添加质量分数及表观气速下,纳米Fe3O4的流诧性能得到改善,其在流化床中形成的大聚团得到有效的破碎,床层膨胀增加,压降趋子一个稳定值,最小流化速度降低,床层可以实现比较均匀的流化。     

CHARACTERIZING FLUIDIZATION BY THE BED COLLAPSING METHOD

The fluidizing characteristic of a powder may be identified by studying the subsidence curve of a fully fluidized bed after abrupt termination of the fluid supply. The full bed collapsing process consists of three consecutive stages: a rapid initial stage for bubble escape, an intermediate stage of hindered sedimentation with constant velocity of solids descent, and a final decelerating stage of solids consolidation. For certain fluid-solid systems, either one or two of these stages may be missing. Mathematical models proposed for the individual stages and corroborated by high-speed cinematographic experimental measurements, led to the formulation of a dimensionless subsidence time Θ, correlating the physical properties of the solids and the fluid as well as the operating parameters to the fluidizing characteristic of the system. The larger the value of Θ, the smoother the fluidization.

For automatic determination of the subsidence behavior of a collapsing bed, an instrument using an optical-fiber projector-receiver set, for rapid tracking and recording of the subsiding bed surface, was developed. When the instrument output was fed into a microprocessor, the relevant parameters defining fluidizing characteristics were computed and displayed. By using this instrument, the fluidizing characteristics of binary mixtures of two closely sized powders were studied. For binary mixtures consisting of Geldart's Group A and Group B powders, fluidizing characteristics were noted to be intermediate between those of the two consistent components according to their relative proportions. When a Group C powder was added to either a Group A or Group B powder, however, the fluidizing characteristic of either component was found to be improved by the presence of the other, and there existed, in general, an intermediate composition with optimum fluidizing characteristic surpassing that of either of the constituents.     

Experimental study on fluidization of fine powders in rotating drums with various wall friction and baffled rotating drums

Fine powders were found to be fluidized in a rotating drum by internal cycling gas by the drum rotation. It is essentially a fluidized bed without requiring any external fluidizing gas. Such a rotating drum can be regarded as a new gasless fluidized bed for fine powders in contrast to a traditional fluidized bed, possibly leading to a considerable amount of energy savings. In addition, the fluidization quality of fine powders was found to be further improved with the assistance of drum rotation because of the shearing movement among particles that eliminates channeling and cracks and possibly also breaks agglomerates. Five regimes were identified in the rotating drum including slipping, avalanching-sliding, aerated, fluidization and re-compacted regimes. It was also found that drum wall friction plays an important role to fluidize fine powders because the friction carries particles to the freeboard, leading to gas cycling that fluidizes the powders. As well, three types of specially designed baffles were utilized to promote powder fluidization in rotating drums. These baffles effectively bring an early onset of all the regimes in rotating drums by reducing powder-wall slipping, carrying particles and bringing additional gas to the powders.     

Solids mixing behavior in a nano-agglomerate fluidized bed

The nano-particles mixing behavior in a nano-agglomerate fluidized bed (NAFB) using R972, a kind of nano-SiO₂ powder, was investigated by the nano-particle coated phosphors tracer method. The axial and radial solids dispersion coefficients in this system were two orders of magnitude lower than those in fluid catalytic cracking (FCC) catalyst systems. The axial solids dispersion coefficient increased with increasing superficial gas velocities, and ranged between 9.1 × 10^− 4 and 2.6 × 10^− 3 m²/s. There was a step increase in the axial solids dispersion coefficient between the particulate fluidization regime and bubbling and turbulent fluidization regimes. As the superficial gas velocity increased, the radial solids dispersion coefficient increased gradually, from 1.2 × 10^− 4 to 4.5 × 10^− 4 m²/s. The much smaller D_a and D_r, compared to regular fluidized systems, is mainly due to the reduced density difference between the fluidized particles and fluidizing medium. To validate this, the solids dispersion coefficients in the NABF were compared with literature values for liquid-solid particulate systems in the particulate fluidization regime and FCC systems in the bubbling and turbulent fluidization regimes. The density difference between the fluidized particles and fluidizing medium and kinetic viscosity of the fluidizing medium, and other hydrodynamic factors like the superficial velocity of the fluidizing medium and the average diameters of the fluidized particles, were the key factors in the solids mixing in the fluidized beds. Empirical correlations are given to describe the results.     

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。     

Interpretation of Geldart's type A,B, C and D powders by taking into account interparticle cohesion forces

By taking into account interparticle cohesion forces, one can derive limiting conditions which result in a classification of powders which is equivalent to the definition given by Geldart [1].Separation of powder type A from powder type C follows from the condition that free particle motion is suppressed by the dominance of cohesion forces in the case of powder type C.Separation of powder group B from powder group A is defined by the unimportance of cohesion forces on fluidization behavior in the case of powders of type B.Separation of powder group D from powder group B is defined by the fact that for minimum fluidization of powders of type D the dynamic pressure of the fluidizing agent exceeds a distinct value depending on particle size and density difference.     

在具有锥形料腿的循环流化床中流化CaCO3超细颗粒

根据粘附性颗粒在流化过程中形成的聚团具有较宽粒径分布并因此导致大聚团在流化床中沉积和死床的问题,提出了循环流化床的锥形回料系统设计. 该回料系统包括两部分：锥形料腿和带辅助进气的V型阀. 实验证明,锥形料腿通过提供变化的表观流化气速,克服了流化聚团沉积死床等现象;而V型阀的辅助进气,对于保证V型阀顺利输送粘附性颗粒具有关键性作用. 借助这种回料系统,实现了高粘附性超细CaCO3颗粒在循环流化床的稳定快速流化. 从提升管内部拍摄的照片显示,尽管提升管采用较高的流化气体速度,但超细CaCO3颗粒仍然是以聚团的形式被流化. 对在提升管不同高度采集的聚团分析表明,处于快速流化状态的CaCO3聚团的直径远小于传统流化床中聚团的直径,并且在提升管高度方向聚团直径没有较大的变化. 同时实验还显示,提升管轴向空隙率呈S型分布,而径向则体现环-核结构,具有典型的快速床特征.