Hydrodynamics of gas-solid fluidized bed of disparately sized binary particles

The hydrodynamics of binary mixture of Geldart Group A and D particles in a turbulent fluidized bed were investigated by experiment and computational fluid dynamics (CFD) method in this paper. The results showed that at low gas velocity, the binary mixtures tend to segregate. At moderate gas velocity, they incline to mix well in the dense phase. Further increasing gas velocity, small particles are entrained and accumulate in the upper regime of the bed, and a segregation trend of the binary mixture appears again. At high gas velocities, segregation efficiency in the continuous classification process increases with increasing the gas velocity and mean residence time of the binary mixture, however, decreases with increasing the small particle content. A strong particle recirculation appears all over the dense phase of the bed, causing an approximately uniform solid composition in radial direction of the fluidized bed.     

Axial segregation in bubbling gas‐fluidized beds with Gaussian and lognormal distributions of Geldart Group B particles

Bubbling, gas‐fluidized bed experiments involving Geldart Group B particles with continuous‐size distributions have been carried out. Sand of various widths of Gaussian or lognormal distributions were completely fluidized, then axial concentration profiles were obtained from frozen‐bed sectioning. Similar to previous works on binary systems, results show that mean particle diameter decreases with increasing bed height, and that wider Gaussian distributions show increased segregation extents. Surprisingly, however, lognormal distributions exhibit a nonmonotonic segregation trend with respect to distribution widths. In addition, the shape of the local‐size distribution is largely preserved with respect to that of the overall distribution. These findings on the nature of local‐size distribution provide experimental confirmation of previous results for granular and gas‐solid simulations. Lastly, an interesting observation is that although monodisperse Geldart Group D particles cannot be completely fluidized, their presence in lognormal distributions investigated still results in complete fluidization of all particles. © 2010 American Institute of Chemical Engineers AIChE J, 2010     

D类颗粒节涌流态化的实验和数值模拟

应用双流体气固两相流模型,对均一粒径分布的Geldart D类颗粒的节涌流态化过程进行了模拟. 研究了流化过程中流化状态转变、床层膨胀比以及压力脉动功率谱,从Froude准数和颗粒动能的角度分析了模拟结果中的流化特性,并与实验数据进行了对比. 模拟结果准确预测了Geldart D类颗粒的节涌流态化特性,对床层膨胀高度和功率谱的预测与实验基本吻合. Froude准数和颗粒动能随时间的周期性脉动较好地反映了流化床内节涌流态化的气泡行为.     

Investigation of Drying Geldart D and B Particles in Different Fluidization Regimes

Drying of nylon (Geldart D) and expanded polystyrene (Geldart B) particles in fixed and fluidized beds were studied experimentally and theoretically. Fluidized bed dryers are sometimes operated at velocities beyond bubbling fluidization to mitigate against de‐fluidization of surface wet particles. It was found that theoretical analysis using three different drying methods could predict the constant‐drying rate at such velocities and also across the entire fluidization regimes (fixed bed, bubbling, slugging and turbulent fluidization) as long as the bed remains completely fluidized. Results also showed that the theoretical predictions were accurate beyond previously reported velocity limits in a laboratory scale dryer. During bubbling fluidization, the cross flow factor method was used effectively to predict the influence of bubble phase on drying rates. In the falling‐rate period, it is demonstrated that the drying behaviour of nylon at different gas velocities can be characterised by a single normalized drying curve.     

Practical validation of the two-fluid model applied to dense gas-solid flows in fluidized beds

This paper discusses the simulation of bubbling gas-solid flows by using the Eulerian two-fluid approach. Predictions of particle motion, bed expansion, bubble size and bubble velocity in bubbling beds containing Geldart B particles are compared with experimental results and correlations found in the literature. In addition, gas mixing in a bed of Geldart A particles is investigated.An in-house code has been developed based on the finite-volume method and the time-splitting approach using a staggered grid arrangement. The velocities in both phases are obtained by solving the 2D Reynolds-averaged Navier/Stokes equations using a partial elimination algorithm (PEA) and a coupled solver. The k-ε turbulence model is used to describe the turbulent quantities in the continuous phase.In general, the model predictions are in good agreement with experimental data found in the literature. Most important observations are: the level of the restitution coefficient was found to be crucial in order to obtain successful results from 2D axisymmetric simulations of a system containing Geldart B particles. Bubble size and bubble rise velocities are not as sensitive to the restitution coefficient. The turbulence model is of outmost importance concerning gas mixing in a fluidized bed of Geldart A particles.From these numerical analyzes an optimized granular flow two-fluid model can be designed for the purpose of simulating reactive systems in fluidized bed reactors.     

Deterministic chaos: a new tool in fluidized bed design and operation

Deterministic chaos theory offers new and useful quantitative tools to characterize the non-linear dynamic behaviour of fluidized beds. The dimension and entropy of the fluidized bed's strange attractor can be used for various purposes, such as the classification of fluidization regimes or fluidized bed scale-up. This is illustrated by experimental and model simulation examples of deterministic chaotic behaviour in ambient gas-solids fluidized beds of Geldart B particles. It is shown that the Kolmogorov entropy is dependent on, amongst other parameters, the gas velocity and the bed aspect ratio. In dimensionless scaling of fluidized bed reactors this type of relationship can probably be of use in establishing full dynamic similarity.     

PVC类废塑料在冷态流化床中流化行为的研究

在Φ50 mm×800 mm圆柱体的冷态流化床反应器中,对PVC类废塑料、石英砂及其混合物的流化特性进行了研究。研究了PVC颗粒粒径与混合物料中PVC质量分数对混合物料的流化特性的影响规律,得到指导热态实验的关键参数。实验结果表明,PVC颗粒粒径与混合物料中PVC质量分数会影响混合物料的最小流化速度,也影响PVC颗粒与石英砂混合的均匀度。混合物料中PVC的质量分数越小,其最小流化速度就越小,混合物料也越容易实现充分混合;PVC颗粒为Geldart B类颗粒,但由于形状不规则,黏性力大,塌落特性明显,流化性能较差,显示出C类颗粒的流化特性,同时实际的最小流化速度要大于理论最小流化速度。PVC与石英砂混合物料冷态流化行为的研究结果为热态流化床降解PVC颗粒提供了基础数据和实践依据。     

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.     

On Geldart Group A behaviour in fluidized beds with and without cohesive interparticle forces: A DEM study

This paper presents a 2D soft sphere discrete element method (DEM) simulation study of fluidization behaviour of Geldart Group A powders and Geldart Group B powders in the presence of externally imposed cohesive interparticle force. In the presence of externally imposed cohesive interparticle force, beds of Group B powders exhibit some of the characteristics of Group A powders (homogeneous bed expansion and pressure drop hysteresis), but show other characteristics (e.g. bed collapse) which are quite different. The homogeneous bed expansion for Group B particles with imposed cohesive interparticle force is found to follow the Richardson-Zaki relationship, with the exponent n being independent of the magnitude of interparticle force and with the degree of expansion increasing with the magnitude of interparticle force. Group A particles show homogeneous bed expansion even in the absence of cohesive interparticle force.     

磷矿颗粒流态化特性的实验研究

在高1 m、内径42mm的流化床中,对粒径54-600 μm、密度2 252-2 665 kg/m3的磷矿颗粒的流态化特性进行实验研究.实验结果表明:磷矿颗粒粒径和密度对磷矿颗粒流态化行为有较大影响,床层膨胀比随着磷矿颗粒粒径的增大而逐渐减小.当磷矿颗粒属于Geldart B类颗粒时,流化较好;而当颗粒平均粒径为82 ...     

Fluidization Characteristics of Silicon Particles with a Wide Size Distribution

Fluidization characteristics of silicon particle system are studied by the pressure fluctuation method. The existence of fine particles in the system can improve fluidization. Silicon particles with a wide size distribution, preferably with some fines, behave as Group A particles according to Geldart classification, although the system belongs to Group B actually. The system is also approved to be suitable for organochlorosilane monomer production using a fluidized bed reactor. Experimental data obtained in this work are important for the design and operation of commercial fluidized bed reactors for the production of organochlorosilane monomers.     

宽筛分硅粉颗粒的流化特性

Fluidization characteristics of silicon particle system are studied by the pressure fluctuation method.The existence of fine particles in the system can improve fluidization. Silicon particles with a wide size distribution,preferably with some fines, behave as Group A particles according to Geldart classification, although the system belongs to Group B actually. The system is also approved to be suitable for organochlorosilane monomer production using a fluidized bed reactor. Experimental data obtained in this work are important for the design and operation of commercial fluidized bed reactors for the production of organochlorosilane monomers.     

Nanoparticle fluidization and Geldart's classification

The behaviour of gas-particle interaction in a fluidized bed depends strongly on the size of the particles being fluidized. Fluidization characteristics of macro-sized particles, from several tens of microns to several millimetres, are well described by the Geldart [1973. Types of gas fluidization, Powder Technology 7, 285] classification. There is evidence that fluidization characteristics of nano-sized particles may be analysed by analogies to those of macro-sized particles. The aim of this paper is to look at whether the mechanism resulting in cohesive behaviour for macro-sized particles may be extended to nano-sized particles. Degussa Aerosil R974 powder, with a primary particle size of 12 nm, was fluidized using nitrogen in a cylindrical vessel, 50-mm-id and 900 mm in height. Characteristics of incipient fluidization are analysed in relation to variations in the initial packed bed conditions. Bed collapse experiments were performed and the results are used for assessing fluidization characteristics of the particles. It was found that nano-sized particles possess characteristics of both Group A and Group C of Geldart classification. Analysis shows that fluidization characteristics of nano-sized particles may be bridged to those of macro-sized particles through particle aggregation.     

Improvement of the Fluidizability of Cohesive Powders through Mixing with Small Proportions of Group A Particles

The gas fluidization behaviour of fine cohesive powders, classified as Geldart group C, is known to be characterized by cracks and channels leading to severe non‐homogeneities in the bed. Geldart group A particles, on the other hand, are known to show more homogeneous and regular fluidization behaviour. This paper studies the effects of the addition of small proportions of group A on the fluidization behaviour of a group C powder. Differential pressure fluctuations data at a sampling frequency of 200 Hz were recorded for two cases. In the first case, the bed contained only group C powder while in the second case small amounts of group A particles were added to the existing group C powder. Visual/image observations coupled with time series analysis showed that the addition of small proportions of group A particles substantially improved the fluidization behaviour of the bed even at low superficial gas velocities, leading to a more uniform fluidization. Evaluation of mean and standard deviations has shown the advantage of mixing the two powders as it allowed larger pressure fluctuations and smaller standard deviations. Power spectra, on the other hand, showed that unlike group C, for which fluctuations were small in magnitude and broadband in structure, the mixture showed stronger periodic behaviour as result of the attenuation of the small and rapid fluctuations caused by the flow of gas in the cracks and channels. Advanced methods such as the principal component analysis of the embedded trajectories allowed a quantitative comparison between the fluidization behaviour of the two systems.     

气-固微型流化床压降特性及最小流化速度的实验研究

在内径3～20 mm的4个气-固微型流化床中,分别考察了A类和B类两种类型颗粒的流化特性,同时研究了床几何结构、操作条件、物相性质等各因素对其最小流化速度的影响.结果 表明,气-固微型流化床中的床层压降特性与颗粒类型密切相关,不同的流动状态下两种类型颗粒的流动特性存在显著地差异.在固定床阶段,与B类颗粒相比,A类颗粒与...     

Control of particle cohesion with a polymer coating and temperature adjustment

A new approach is presented that introduces interparticle forces induced by a change of temperature at which polymer coated particles are exposed. The particle cohesive flow behavior is shown for two different applications. The first one considers a dense granular flow that is typically observed for wet powder granulation using a modified spheronizer. The other application shows the possibility of mimicking the particle flow behavior observed in high‐temperature fluidized beds with the advantage of being operated at ambient conditions. For the first application, as the temperature increases, significant changes in the particle bed surface morphology were observed and an important reduction of the dynamic density was noticed. For the gas–solid fluidized‐bed application, pressure drop measurements revealed that the behavior of the particles transited from Geldart group B to Geldart group A and even Geldart group C as the temperature increased. © 2012 American Institute of Chemical Engineers AIChE J, 2012     

Experimental and numerical investigation of sands and Geldart A biomass co-fluidization

This article investigated the fluidization of sands and small Geldart A biomass mixtures. The mixture fluidized like Geldart A type particles with a uniform bed expansion regime before bubbling. The video recorded color distance between pure sands and sands–biomass mixtures was used to estimate the sands–biomass mixing. The coarse-grained computational fluid dynamics–discrete element method with a hybrid drag model which couples the Syamlal–O'Brien drag and a filtered drag can capture the mixing while the simulation with Gidaspow drag predicted a segregated bed. The simulations were further validated with experimental measured pressure drops. The time averaged pressure drop equals the weight of the bed material, however, its fluctuation is about three times of the bed material fluctuation.     

节涌流化床中气栓行为的混沌分析

研究显示节涌流化床中的气栓行为具有混沌特征 ,而且其混沌特征参数 (关联维与关联熵 )随着气速的增加呈“W”型变化趋势。“W”型中的两个低点预示着气栓运动状态的转变     

Modification and re-interpretation of Geldart's classification of powders

In developing his powder classification, Geldart [D. Geldart, Powder Technol. 7 (1973) 285.] employed fluidization data obtained only at ambient temperature and pressure and from beds fluidized only with air. Unfortunately, industrial applications of fluidized bed technology invariably are at elevated pressure and temperature and with fluidizing gas other than air. Geldart classification of powders does not apply at elevated pressure and temperature. There are ample evidences reported in the literature indicating that normally Geldart Group B powders at ambient conditions, such as polymer particles, can behave like a Group A powder under polymerization conditions at elevated pressure and moderate temperature with substantial emulsion-phase expansion, relatively small bubbles, smooth fluidization, and reduced gas bypassing [J.R. Grace, Can. J. Chem. Eng. 64 (1986) 353; I.D. Burdett, R.S. Elsinger, P. Cai, K.H. Lee, Gas-phase fluidization technology for production of polyolefins, in Fluidization X, Eds. M. Kwauk, J. Li, W.C. Yang, 2001, pp. 39-52; P.N. Rowe, P.U. Foscolo, A.C. Hoffmann, J.G. Yates, X-ray observation of gas fluidized beds under pressure, in Fluidization IV, Eds. D. Kunii, R. Toei, 1983, pp. 53-60]. Similar findings were also reported for Geldart Group B powders fluidized by supercritical carbon dioxide at elevated pressures [C. Vogt, R. Schreiber, J. Werther, G. Brunner, Fluidization at supercritical fluid conditions, in Fluidization X, Eds. M. Kwauk, J. Li, W.C. Yang, 2001, pp. 117-124; C. Vogt, R. Schreiber, G. Brunner, J. Werther, Powder Technol. 158 (2005) 102; D. Liu, M. Kwauk, H. Li, Chem. Eng. Sci. 51 (1996) 4045; M. Poletto, P. Salatino, L. Massimilla, Chem. Eng. Sci. 48 (1993) 617; A. Marzocchella, P. Salatino, AIChE J. 46 (2000) 901].The original Geldart's classification is modified and re-interpreted in this paper by plotting a dimensionless density against the Archimedes number. The new parameters allow powders with different properties fluidized at different pressures and temperatures with gases of different properties to be plotted in the same graph. The proposed modification successfully transforms the normally Geldart Group B particles at ambient conditions to Group A classification when fluidized at elevated pressure and temperature. The selection of these two parameters, the dimensionless density and the Archimedes number, for plotting is not arbitrary, however. The experimental and theoretical development is discussed.     

Geldart A类颗粒节涌床气固流动特性的实验及模拟

针对气固节涌床,在实验基础上,基于欧拉?欧拉双流体模型结合颗粒动力学理论,考虑Geldart A类颗粒聚团对气固间曳力的影响,采用修正后的Gidaspow曳力模型对气固节涌床进行数值模拟。结果表明,通过与实验结果及经验公式进行对比,修正的模型可准确合理地模拟流化床内节涌特性。表观气速0.09 m/s≤Ug≤0.39 m/s时,床层内部压力脉动标准偏差随表观气速增加而增加,流型由鼓泡转变为节涌直至节涌程度最大,床内气固流动主要受轴对称栓运动特性影响,床内压降、床层膨胀比、气栓平均上升速度、最大轴对称栓长度随表观气速增加而增加,最大轴对称栓产生位置随表观气速增加而降低;Ug>0.39 m/s后,床内压力脉动标准偏差随表观气速增加而降低,节涌程度降低至向湍动流态化流型转变,床内气固流动主要受壁面栓运动特性影响,增加表观气速,节涌床内压降变化幅度较小,气栓平均上升速度增加幅度加大,床层膨胀比及最大轴对称栓长度降低,最大轴对称栓产生的位置略有升高。