The mechanics of spout-fluid beds at the minimum spout-fluid flowrate

Equations for predicting the minimum fluid flowrate in spout-fluid beds of coarse spherical particles are developed and experimentally verified. Correlations for the spout diameter and maximum spoutable height are also given. The annular pressure drop equations developed in previous work are experimentally verified.     

Jet penetration depth in a two-dimensional spout-fluid bed

The jet penetration depth was proposed to be an important parameter to describe the jet action during the chemical process of spout-fluid bed coal gasification. A two-dimensional cold model of a spout-fluid bed coal gasifier with its cross section of and height of 2000 mm was established to investigate the jet penetration depth. Four types of Geldart group D particles were used as bed materials. A multi-channel pressure sampling system and a high-resolution digital CCD camera were employed for experimental investigations. The effects of spouting gas velocity, spout nozzle diameter, static bed height, particle property and fluidizing gas flow rate on the jet penetration depth have been systematically studied by pressure signal analysis and image processing. Experimental results indicate that the jet penetration depth increases with increasing spouting gas velocity and spout nozzle diameter, while it decreases with increasing particle density, particle diameter, static bed height and fluidizing gas flow rate. Additional, a new correlation considered all of the above effects especially static bed height and fluidizing gas flow rate, was developed for predicting the jet penetration depth in spout-fluid beds. The correlation was compared with published experimental data or correlations, which was in well agreement with the present experimental results and some other references.     

导向管喷动流化床的喷动气旁路分率

在内径为182 mm的喷动流化床中安装内径80 mm的导向管,以平均粒径为2.2 mm的尿素颗粒为物料,对喷动气旁路特性进行了实验研究,分别考察了夹带区高度、导向管长度、喷嘴内径、床层高度、喷动气速和流化气速对喷动气旁路分率的影响,结果表明随着喷动气速的增大,喷动气体旁路分率先增后减。导向管安装高度越高,气体旁路分率越大。床层高度增大喷动气体旁路分率略有降低。而喷嘴直径小于50 mm时气体旁路分率随喷嘴直径增大而提高,在大于50 mm时气体旁路分率随喷嘴直径增大维持不变。当气速较小时,导向管高度增大会引起气体旁路分率增大,引入少量流化气能有效地抑制喷动气旁路。     

基于信息熵分析的喷动流化床流动特性

建立了300 mm×30 mm×2000 mm的喷动流化床煤气化炉冷态实验装置和多通道压力信号采集系统,引入压力波动时间序列的Shannon信息熵分析,讨论了不同喷动气速度和流化气流率下各床层区域的Shannon 信息熵,并结合高分辨率数码CCD相机所记录的流动状态,建立了Shannon信息熵与流型之间的联系.床层不同区域的Shannon 信息熵具有较大的差异,不同流型的Shannon 信息熵区分度较好.在较高的喷动气速度或流化气流率下,喷动流化床气固运动周期特性消失,呈现出明显的混沌特性,表现为床层各区域Shannon信息熵的急剧增长和床内不稳定的流动状态的发生.结果表明,Shannon信息熵分析有助于认识喷动流化床复杂的流型及其转变和床内气固两相流动的混沌动力学特性.     

Fluid flow pattern and solids circulation rate in a liquid phase spout-fluid bed with draft tube

The fluid flow pattern and solids circulation rate in a liquid phase spout-fluid bed with a draft tube were studied in a semi-circular column 196 mm in diameter equipped with a semi-circular draft tube 34.5 mm in diameter using water and spherical glass particles 1.20, 1.94 and 2.98 mm in diameter. Both the solids circulation rate and fluid distribution between the draft tube and the annulus are influenced by the location of the draft tube, the relative magnitude of the inlet spouting and annulus flowrates, and the total fluid flowrate entering the bed. A one-dimensional steady state model of vertical non-accelerating liquid-solids flow predicts the solids mass flux in the draft tube with a mean deviation of 12.3% when experimental values of the axial pressure gradients in the draft tube and annulus are specified. A simple correlation for the fountain height is also presented.     

Characterization of dynamic behavior of a spout-fluid bed with Shannon entropy analysis

Differential pressure fluctuation time series were obtained at different locations in a two-dimensional spout-fluid bed with a cross section of 300 × 30 mm and height 2000 mm. Shannon entropy analysis of differential pressure fluctuations was developed to characterize the dynamic behavior. Effects of two important operating parameters (spouting gas velocity and fluidizing gas flow rate) on the Shannon entropy were examined. It was demonstrated that a spout-fluid bed at a high spouting gas velocity or fluidizing gas flow rate was a deterministic chaos system since the Shannon entropies at all bed locations increased sharply and asymmetric unstable flows occurred. Shannon entropies were found to be significantly different at various bed locations. Shannon entropies of different flow regimes were distinct, so they were used to identify the flow regimes. The results show that the Shannon entropy helps to grasp the complex characteristics of dynamic behavior in spout-fluid beds.     

Solids circulation in a spout-fluid bed with draft tibe

A 20 cm diameter semi-cylindrical spout-fluid bed with a draft tube has been used to study the effects of operating and geometric parameters on the solids circulation rates at ambient temperature. A new technique has been developed for measuring the solids fluxes with great accuracy. Solids circulation rate data have been found to be strongly influenced by both geometry and relative magnitude of spouting and auxiliary gas flowrates, as they in turn affect the flow of the gas-solid mixture inside the draft tube. The solids circulation rate was greatly enhanced when an auxiliary flow aerated the annular region and such enhancement has been found to be linearly dependent on the auxiliary flow contribution to the total gas flow and on the distance between the base of the draft tube and the inlet nozzle.     

喷动－流化床床层压降及其最优化操作探讨

在内径为０．１３９ｍ的有机玻璃床内，以空气为流化介质，分别对两类河砂作了喷动流化的不同操作──固定喷动气流量Ｑ＿ｓ（喷嘴内径０．０１９ｍ）、调节环形区流化气流量Ｑ＿Ｆ和固定Ｑ＿Ｆ调节Ｑ＿ｓ的操作，通过对床层压降变化的探讨．提出喷动－流化床的最优化操作。     

喷动－流化床床层压降及其最优化操作探讨

在内径为０．１３９ｍ的有机玻璃床内，以空气为流化介质，分别对两类河砂作了喷动流化的不同操作──固定喷动气流量Ｑ＿ｓ（喷嘴内径０．０１９ｍ）、调节环形区流化气流量Ｑ＿Ｆ和固定Ｑ＿Ｆ调节Ｑ＿ｓ的操作，通过对床层压降变化的探讨．提出喷动－流化床的最优化操作。     

Spoutable bed height and pressure fluctuation of a novel annular spouted bed with V-shaped deflector

A novel annular spouted bed consisting of two homocentric upright cylinders with different diameters was developed. The nozzles and V-shaped deflectors were located in the bottom of annular space between the inner and outer cylinders. The effects of hold-up, bed material, total flowrate and nozzle structure on the hydrodynamic characteristics of the novel annular spouted bed were investigated. The results show that there exist three different zones for the particle flow in the annular spouted bed: the moving packed zone, the dense-phase spouted fluidizing zone and the dilute-phase zone. With the increase of hold-ups, the height of the dense-phase spouted fluidizing zone tends to increase in the annular spouted bed, while the moving packed zone is only limited within the V-shaped deflectors. The maximum spoutable amount for high air flowrate is larger than that for low air flowrate. Both the spoutable bed height and the local mean relative pressure for high air flowrate are higher than those for low air flowrate at the same hold-ups of particles. The nozzle structure also has important effects on the spoutable bed height and the local relative pressure in the annular spouted bed.     

Separation and residence times of larger particles in a spout-fluid bed

Optimum conditions for the separation of added large particles from a spout-fluid bed of Geldart Type B powder have been determined. A shallow bed, 100 mm in diameter, with porous conical distributor was used. Mean and distributions of residence time of the large particles depend on the two gas flow rates, especially that to the distributor, and on spout inlet diameter and large particle size. Bed regimes studied were mainly spouting with aeration and spout-fluidization. In the latter regime an optimum range of fluidizing gas flow rates that minimised mean and spread of residence times was identified. RTD data were correlated by a model incorporating a minimum time supplemented by a distribution for an ideally mixed system.     

喷动流化床最大喷动压降的多因素影响与关联

基于截面200 mm×20 mm,高1600 mm,锥角60°的矩形喷动流化床,以二组分混合颗粒、单一组分球形颗粒及非球形颗粒为物料进行最大喷动压降的实验研究.结果表明,最大喷动压降随静止床高、颗粒密度、颗粒球形度及二组分混合颗粒体系中沉积组分分率增加而增大,随流化气速增大而减小;增大颗粒粒径或喷口宽度,呈现先减小后增...     

Pressure and flow characteristics of a gas phase spout-fluid bed and the minimum spout-fluid condition

Spoutfluidization is a new technique for solid-fluid contact which aims at incorporating the advantages of spouted bed and fluidized bed technique. The characteristics of physical state of the bed with the variation of the variables which include flow of fluid, particle diameter, orifice diameter, bed height, are studied in this investigation. Experimental study of minimum spoutfluidizing velocity using glass beads with mean particle diameters from 0.254 to 0.600 mm has been carried out in a 90 mm glass column with three spouting inlet orifice sizes at different bed heights. Phase diagrams indicate that the minimum spout-fluid flow rate in a gas-solid system may be a point property for a given bed. A correlation is presented in which the standard deviation of experimental from calculated minimum spoutfluidizing velocity is within 5%.     

Prediction of the maximum spoutable bed height in spout-fluid beds

A model for predicting the ratio of the maximum spoutable bed height in a spout-fluid bed to the maximum spoutable bed height in a spouted bed is presented and experimentally verified. The model is a further extension of the basic Mamuro and Hattori force balance model. The ratio H_mSF/H_m is found to be a function of the external annular fluid flowrate and a parameter C, which is the ratio of fluid velocity at the top of the annulus to that at minimum fluidization. C = 0.935 gives a best fit of our data.     

Minimum fluid flowrate,pressure drop and stability of a conical spouted bed

A model for calculating the minimum spouting flowrate and pressure drop in a conical spouted bed has been developed and described in our previous paper (Had?ismajlovi et al., 1986). In the present work, this model was examined at a wider range of experimental conditions and it was found that measured and predicted values of the minimum spouting flowrate and pressure drop differed by about 10.3% and 20.0%, respectively. It is shown that the spouted bed in a conical column is stable when the inlet tube diameter is less than 25 particle diameters.     

DEM simulation of particle mixing in flat-bottom spout-fluid bed

The particle mixing mechanism affects the rate of the process and the achievable homogeneity. This paper presents a numerical study of the particle motion and mixing in flat-bottom spout-fluid bed. In the numerical model, the particle motion is modeled by discrete element method (DEM) and the gas motion is modeled by κ–? two-equation turbulent model. Validation with experiments is first carried out by comparing solid flow pattern and bed pressure drop at various gas velocities. Then, particle velocities, obtained from DEM simulations, are presented to reveal the mixing mechanisms. On the basic, the dependence of mixing index on the time and the effect of gas velocity on mixing and dead zone (stagnant solid) are discussed, respectively. The results indicate that the spouting gas is the driving force for the formation of particle circulation roll, resulting in the mixing. The convective mixing caused by the motion of circulation roll, shear mixing induced by the relative move of circulation rolls and diffusive mixing generated by random walk of particle among circulation rolls are three different mixing mechanisms in spout-fluid bed. The increase of spouting gas velocity promotes the convective and shear mixing. While increasing the fluidizing gas velocity improves significantly the convective mixing and but weakens the shear mixing. Both of them yield a reduction in the dead zone.     

喷动流化床的最小喷动流化速度和床层压降

在一喷动流化床（直径 ５０ ｍｍ）实验台上采用 ０．６３～１．６０ ｍｍ的神府原煤颗粒,在连续进料的情况下进行了最小喷动流化速度以及固定流化气、改变喷动气和固定喷动气、改变流化气的床层压降变化的实验研究．结果表明,最小喷动流化速度可以参考鼓泡流化床的临界流化速度的计算方法;床层压降变化证实,喷动流化床具有良好的调节能力．     

喷动流化床流动特性数值模拟

为了捕捉喷动流化床中微观层次上的颗粒运动信息,建立了基于CFD的二维非稳态喷动流化床欧拉-欧拉两相流模型。分析了不同流化气速对喷动流化床气固流动特性的影响,即不同工况下的炉内压力降、颗粒浓度、床内空隙率分布、气体速度分布和固体颗粒速度分布。数值模拟研究结果表明:随流化气速的增大,压降和炉内平均空隙率逐渐增大,密相床层高度逐渐增加,沿着轴向方向的气体流量增大,喷动气的射流深度逐渐增加,同时射流半径也逐渐增加。     

Pressure distribution in spout-fluid bed reactors

The occurrence of several flow regimes in spout-fluid beds was investigated. Four different flow regimes, viz. a packed bed flow regime, a bubbling and a fluctuating spouted bed flow regime and a stable spouted bed flow regime, were found to exist. Pressure distributions in a spout-fluid bed were measured in several of these flow regimes by means of a moveable pressure probe. A theoretical model that describes the flow pattern in spout-fluid beds was developed from fundamental relationships that govern the flow of gases through porous media. Pressure distributions calculated from this model agree fairly well with measured values.     

Pressure drop,bed expansion and liquid holdup in a three phase spouted bed contactor

Data on the pressure drop, bed expansion and liquid holdup in a three phase spouted bed contactor with an initial bed height of 243 mm. were obtained as a function of the gas and liquid flowrate. Polyethylene spheres 10 mm. in diameter with a density of 320 kg/m³ were spouted in a 194 mm. column using a 30 mm. nozzle. The spouted bed contactor with gas and liquid mass flow-rates of 2.18 and 1.88 kg/m² sec, respectively had similar pressure drop per unit area of particle surface, total liquid holdup per unit volume of operating bed, and “active” holdup, as a fluidized contactor.