旋流筛板式气固挡板流化床内压力脉动特性

在表观气速Ug=0.04~1.14 m/s时,采用旋流筛板构型的挡板式内构件,通过对比分析旋流筛板式气固挡板流化床与自由床内流动现象、压差脉动标准偏差和压力脉动标准偏差等参数,确定了旋流筛板式气固挡板流化床能有效破碎气泡的流动与操作条件。结果表明,构件下方区域颗粒随表观气速增加而不断转移至构件上方床层,造成构件下方区域密相床层高度持续降低,该区域出现3种流动状态并直接决定构件是否能破碎气泡。当Ug<0.44 m/s时,构件下方区域密相床层料位较高,形成下部为密相床层、上部为密相与大气泡交替通过构件的鼓泡床,此时构件具有抑制气泡生长并破碎气泡的作用,全床压差脉动及压力脉动标准偏差低于相同条件下的自由床;当0.44≤Ug<0.66 m/s时,密相床层料位较低,形成下部为密相床层、上部为单一稀相的湍动床,此时构件不再直接抑制气泡生长或破碎气泡,但构件下方密相床层的存在能降低构件下方及构件上方一定高度内床层的压力脉动强度;当Ug≥0.66 m/s后,密相床层完全消失,形成气体为连续相的稀相流化状态,构件不能破碎气泡、降低床层压力和压差脉动强度。     

基于EMMS模型的气固鼓泡床的模拟及气泡特性的分析

基于EMMS曳力模型,采用双流体的方法对气固鼓泡床内的气固流动特性进行模拟,建立基于图像处理气泡特性的分析方法,重点研究了不同表观气速下气泡在床层内分布特性,包括气泡平均当量直径、气泡速度和气泡球形度的轴向分布,以及气泡的生命周期。研究结果表明,小气泡多集中在床层底部和壁面区域,而大气泡多集中在床层中间区域。随着表观气速的增加,床层高度不断增加,气泡的球形度降低,气泡的大小、出现频率、上升速度以及生命周期均增加;然而,当表观气速增大到一定程度,继续增加气速对气泡的上升速度影响不大。     

基于EMMS模型的气固鼓泡床的模拟及气泡特性的分析

基于EMMS曳力模型,采用双流体的方法对气固鼓泡床内的气固流动特性进行模拟,建立基于图像处理气泡特性的分析方法,重点研究了不同表观气速下气泡在床层内分布特性,包括气泡平均当量直径、气泡速度和气泡球形度的轴向分布,以及气泡的生命周期。研究结果表明,小气泡多集中在床层底部和壁面区域,而大气泡多集中在床层中间区域。随着表观气速的增加,床层高度不断增加,气泡的球形度降低,气泡的大小、出现频率、上升速度以及生命周期均增加;然而,当表观气速增大到一定程度,继续增加气速对气泡的上升速度影响不大。     

加压二维鼓泡床气固流动特性的数值模拟

采用欧拉双流体模型模拟了加压下二维鼓泡床内的气固流动特性,结果表明:在相同的表观气速下,加压使气泡体积分数增大,气泡相与乳化相间的分解越发明显,气固两相流动、混合剧烈;同时,床层中上部颗粒轴向速度的径向分布不均匀性增强:中心区颗粒速度增加,近壁区下降;随着操作压力变大,流化床膨胀高度增大,相应地,整体气含率增大,床层下部的颗粒浓度减小,而上部颗粒浓度增加,固含率在轴向上的分布更均匀;床层压力波动主要由两种成分构成:低频率高幅值和低幅值高频率成分.压力脉动强度随床高的增加呈现先增大后迅速减小的趋势;此外,加压下床层压力脉动强度变大,即床压波动更加剧烈;而且加压下颗粒拟温度增大,即颗粒速度脉动增强.     

采用改进的曳力模型模拟2D鼓泡流化床的流化特性

针对特定颗粒浓度范围颗粒团聚作用导致的曳力下降问题,基于传统曳力模型在不同颗粒浓度段的特性分析,选择适用于不同颗粒浓度区间的曳力模型,通过光滑函数得到改进的曳力模型,并耦合欧拉双流体模型对2D鼓泡流化床进行数值模拟. 结果表明,与Gidaspow和Syamlal-O'Brien模型相比,改进的曳力模型对床层局部压降的预测结果更好;随表观气速增加,改进的曳力模型能更准确地预测床层膨胀;当表观气速Ug=0.46 m/s时,改进的曳力模型对径向颗粒浓度分布的模拟结果明显好于Syamlal-O'Brien模型.     

气液固三相流化床层膨胀特性实验分析

为分析气液固三相流化床床层特性,选用两种粒径接近、密度不同的颗粒:塑料颗粒(湿堆积密度1 273 kg/m~3,平均直径750μm)和陶粒(湿堆积密度1 680 kg/m~3,平均直径800μm),以常温空气为气相、水为液相。实验装置内径0.13 m,全床高度4.75 m,实验液柱高度3.5 m,床内颗粒有足够的膨胀高度。分别测试了液速0—13 mm/s,气速0—12 mm/s条件下的床层高度,研究气液速对塑料颗粒和陶粒床层膨胀率的影响。研究结果显示液速较低时床层收缩,随着气速增加,收缩率增大;液速较高时,膨胀率大于0,随着表观气速的增加,膨胀率先降低,表观气速大于临界值后,膨胀率将增大;除高气速外,床层膨胀率总是随着液速的升高而增大。相同气速、液速条件下,大密度陶粒的床层膨胀(收缩)率大于塑料颗粒。     

气固流化床外取热器内流动和换热特性分析

外取热器是维持催化裂化反应-再生系统热平衡和保持装置平稳运行的关键设备之一。外取热器的优化设计和合理调控，要求深入理解外取热器内的流动特性、换热特性及两者之间关系。在一套大型冷模热态实验装置上，分别考察了表观气速、颗粒质量流率对换热管附近的局部固含率和气泡频率、床层与换热管间传热系数的影响。结果表明：增加表观气速可以降低局部固含率、增加局部气泡频率、强化床层与换热管间换热；随着颗粒质量流率增加，局部固含率和局部气泡频率均增加；在较低表观气速下，增加颗粒质量流率不利于换热，而在较高表观气速下，传热系数随颗粒质量流率逐渐增加。不同流型下，气固流动特性对换热特性的影响不同。在鼓泡床流型下，过高的局部固含率不利于颗粒在换热表面的更新，增加换热管附近的局部气泡频率可以明显强化换热；而在湍流床流型下，换热管附近的局部固含率和气泡频率的增加，均使传热系数逐渐增大。建立了针对不同流型的换热经验关联式，预测值与实验值的平均相对偏差分别为6.9%和1.3%。     

气固流化床内费托铁基催化剂的流化特性

为研究费托(Fischer?Tropsch, FT)催化剂在气固流化床内的流动过程,分析了催化剂的主要物性参数,在不同直径流化床内测量了各表观气速下FT催化剂的流动特性,并与广泛应用的流化催化裂化(Fluid Catalytic Cracking, FCC)催化剂的流态化行为进行了对比。结果表明,同为A类颗粒,相较于FCC催化剂,由于FT催化剂的休止角较小(约为FCC催化剂的75%),其临界流化速度较小、床层膨胀高度和气节高度较小;两种催化剂在流化床内流化过程基本相似,随表观气速增大依次出现膨胀、鼓泡、湍动等流型,但各流型转变时的临界速度差异较大。催化剂物性参数对流化特性影响较大,FT催化剂在各阶段流化过程均相对稳定,有利于催化剂在流化床内均匀分布,其气固接触效果优于FCC催化剂;不同催化剂床层高径比下气节高度变化的转折点与流型存在对应关系,可将气节高度随表观气速的变化关系作为判断湍动流化区内流型临界速度的依据。     

旋流筛板式气固挡板破碎气泡的作用域

为了考察多孔筛板和单旋导向挡板组合对气固两相流动的作用效果,采用床层段内径为90 mm的三维流化床冷模装置,在表观气速(U_g)为0.04～1.14 m/s、初始装料高度(H)为650 mm的操作条件下,分析了自由流化床内气固两相流动特点,并对比分析了自由流化床、单旋流筛板式气固挡板流化床及双旋流筛板式气固挡板流化床压力脉动标准偏差和压差脉动标准偏差等参数,确立了旋流筛板式气固挡板有效抑制并破碎气泡的作用域。结果表明:旋流筛板式气固挡板有效抑制并破碎气泡的气速作用域为0.04 m/s≤U_g≤0.57 m/s,此时对应的自由流化床中气固两相处于鼓泡-节涌过渡流态化;轴向空间作用域为旋流筛板式气固挡板下方及包含旋流筛板式气固挡板的区域。增加旋流筛板式气固挡板的数量有助于强化破碎气泡的效果及拓宽其轴向空间作用域,但并不能拓宽破碎气泡的气速作用域。     

提升管与气-固环流床层耦合反应器的流体力学特性及流动模型

针对催化汽油辅助反应器改质降烯烃技术,在一套提升管与气-固环流床层耦合反应器大型冷模实验装置上,研究了上部环流床层的流体力学特性。结果表明,在环流床层与提升管耦合操作的情况下,床层内颗粒环流存在两种推动力,分别为静压差推动力和颗粒喷射推动力;环隙与导流筒之间的整体平均固含率差随导流筒表观气速增加而增加,随颗粒外循环强度增加而降低;颗粒环流速度随导流筒表观气速和颗粒外循环强度增加而增加。通过对环流床层进行动量衡算,建立了提升管与环流床层耦合流动的数学模型,模型平均相对误差在15.95％以内。     

节涌流化床的压力波动特性

实验研究了流化床流型结构与压力波动的关系,测定了节涌流化床气栓和料栓内的压力波动特性。实验结果表明节涌流化床气泡内压力并非常数而是波动的,但不存在压力梯度,这对进一步认识流态化两相理论有重要意义。     

Fate of solids fed pneumatically through a jet into a fluidized bed

Solid tracer particles were fed pneumatically through a jet into a fluidized bed to simulate the feeding of solids via a pneumatic transport line into a fluidized-bed reactor operating in the slugging-bed mode. The fluidized bed was defluidized instantaneously at different times after the initiation of the tracer particle injection. The bed was then sampled layer by layer to provide the radial and axial concentration profiles of the tracer. Regular and high-speed movies (1,000 frames per second) were taken to study the operation of the fluidized bed and the phenomena of the gas-solid two-phase jet. Experimental results on solid mixing, jet constriction and slugging frequencies, slugging bed height, slug length, jet penetration, and jet half-angle at three nominal jet velocities of 52, 37, and 25 m/s and corresponding solids loadings are presented. Additional experimental results on jet constriction and slugging frequencies, and slug volume (axial slug size) obtained for a wider range of jet velocities confirm the hydrodynamic trends observed during the tracer particle injection experiments. The results indicate that solids mixing increases, and well-mixed conditions are reached earlier, with an increase in jet injection velocity. The obtained mixing times were correlated successfully in terms of the excess gas velocity. The experimental data on jet penetration and slug motion were satisfactorily correlated by modified versions of existing theoretical relations. The modifications included the effect of the injected solids on jet penetration and jet half-angle and also the effect of our semicircular column geometry and single wall-slug configuration on the observed slug motion.     

Characteristics of slug flow in a fluidized bed of polyethylene particles

The slug flow behavior of polyethylene particles was examined in a fluidized bed of 7 cm ID and 50 cm in height. The employed polymer particles were high density polyethylene (HDPE) with the average particle size of 603 μm. The slugging flow of polyethylene particles was analyzed from the measured pressure drop signals by classical statistical methods such as absolute average deviation, probability density function, power spectrum, auto-cor-relation, and cross-correlation. The results show that in spite of high dielectric constant of polymer particles, the slugging phenomena such as incipient slugging velocity, slugging frequency and slugging rise velocity were very similar to the Geldart B type non-polymeric particles. It was observed that slug frequencies decreased with gas velocity and the limiting slug frequency was observed for the gas velocities in this study.     

Effect of temperature on slug properties in a gas fluidized bed

In order to understand the effect of temperature on slug properties, the onset velocity of slugging, slug rising velocity and slug frequency have been measured by a differential pressure method in an electrically heated gas fluidized bed of 0.1 m i.d. and height of 1.97 m and, with respect to variations in gas velocity (U_mf∼0.15 m/s) and temperature (25-400 °C). Air was used as fluidizing gas and fluid catalytic cracking (FCC) catalyst particle (Geldart's group-A particle, d_p=0.071 mm, ρ_p=1600 kg/m³) as bed material. The minimum slugging velocity was found to increase a little with bed temperature. The qualitative change in minimum slugging velocity was found to agree with the inverse of minimum fluidizing velocity as temperature was varied. As the bed temperature increased, slug frequency was found to decrease a little, whereas slug rising velocity increased. A correlation between slug rising velocity and bed temperature was proposed.     

Experimental and numerical research for fluidization behaviors in a gas–solid acoustic fluidized bed

The effects of sound assistance on fluidization behaviors were systematically investigated in a gas–solid acoustic fluidized bed. A model modified from Syamlal–O'Brien drag model was established. The original solid momentum equation was developed and an acoustic model was also proposed. The radial particle volume fraction, axial root‐mean‐square of bed pressure drop, granular temperature, and particle velocity in gas–solid acoustic fluidized bed were simulated using computational fluid dynamics (CFD) code Fluent 6.2. The results showed that radial particle volume fraction increased using modified drag model compared with that using the original one. Radial particle volume fraction was revealed as a parabolic concentration profile. Axial particle volume fraction decreased with the increasing bed height. The granular temperature increased with increasing sound pressure level. It showed that simulation values using CFD code Fluent 6.2 were in agreement with the experimental data. © 2009 American Institute of Chemical Engineers AIChE J, 2010     

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。     

含内构件的循环流化床的动态压力特性

针对含内构件的循环流化床,以石英砂为物料,使用动态压力传感器测量了含内构件的流化床中气固两相流的动态压力,分析了床内的瞬时压力特性. 结果表明,在进出口总压降中,文丘里压降最大,占主床压降的60%以上. 表观气速和固体颗粒循环流率共同影响循环流化床内的压力特性. 压力瞬时波动功率谱分析表明,压力波动对应一个主频,表观气速越小、颗粒循环流率越大时,压力波动越大,且循环流化床底部压力波动比上部大. 加入内构件能有效引导气流,使流动更均匀.     

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...     

循环流化床内颗粒的加速作用及气固两相间的动量交换

根据对气固两相流动特性的分析,表明在循环流化床提升管内,颗粒的加速运动及气固两相间的动量交换对床层各项参数具有明显的影响。由于颗粒聚集,减小了气固两相间的相互作用,使曳力系数小于单颗粒标准曳力系数(C_D/C_(DS)<1.0)。从而使颗粒具有较长的加速段,其加速压降在总压降中所占的分率不可忽略。考虑颗粒加速作用及由于颗粒聚集使气固两相相互作用力减小的事实后,用一维轴向稳态流动的模型可以获得截面平均空隙率、平均颗粒速度以及曳力系数等参数及其轴向分布规律,并与实验直接测定结果吻合很好。通过对大量数据的分析,表明C_D/C_(DS)可用下述经验关联式表示:C_D/C_(DS)=1.68(ε)~(0.253)(Re_(?)/Re_t)~(-1.213)(d_P/D)~(0.105)