小管径-粒径比颗粒无序堆积通道内壁面效应数值研究

采用DEM-CFD方法对小管径-粒径比颗粒无序堆积通道内壁面效应进行了数值研究。针对D/d_p=5.0圆球无序堆积通道构建了光滑壁面和波节壁面两种通道壁面结构,分析了不同壁面结构堆积通道内孔隙率分布、流动和温度场分布及其流动换热性能。结果表明：小管径-粒径比光滑壁面颗粒无序堆积通道内壁面效应显著,壁面附近平均流速明显高于堆积中心区域,而平均温度要低于堆积中心区域,壁面附近0.5d_p区域内通过的流体质量流量比例为46%;波节壁面结构抑制了通道壁面附近漏流,可小幅提高堆积通道的换热能力,但堆积通道内的流动阻力也随之增大,其综合换热性能较光滑壁面堆积通道有所下降。     

小管径-粒径比颗粒无序堆积通道内壁面效应数值研究

采用DEM-CFD方法对小管径-粒径比颗粒无序堆积通道内壁面效应进行了数值研究。针对D/dp=5.0圆球无序堆积通道构建了光滑壁面和波节壁面两种通道壁面结构,分析了不同壁面结构堆积通道内孔隙率分布、流动和温度场分布及其流动换热性能。结果表明:小管径-粒径比光滑壁面颗粒无序堆积通道内壁面效应显著,壁面附近平均流速明显高于堆积中心区域,而平均温度要低于堆积中心区域,壁面附近0.5dp区域内通过的流体质量流量比例为46%;波节壁面结构抑制了通道壁面附近漏流,可小幅提高堆积通道的换热能力,但堆积通道内的流动阻力也随之增大,其综合换热性能较光滑壁面堆积通道有所下降。     

旋转填料床气相流场数值模拟

为解决旋转填料床内部流场较为复杂,实验流体力学基础理论研究缺乏的问题,通过计算流体力学软件FLUENT,采用正交试验法研究了填料转速、气体进口速度和填料的孔隙率对于气体流场径向速度不均匀系数的影响情况。结果表明,当填料转速1 000 r/min、气流速度2 m/s、填料孔隙率0.5时,能使径向速度保持最好的均匀性分布,同时影响RPB截面径向气流速度均匀性按显著程度依次为填料孔隙率〉气体进口速度〉填料转速。     

基于CFD-DEM的异形催化剂径向床反应器数值模拟

为研究催化剂颗粒形状对床层流场均匀度的影响,应用计算流体力学-离散元耦合方法(CFD-DEM)对异形催化剂颗粒随机堆积径向床反应器内的流场进行数值模拟,分别建立柱形、小孔环柱形、大孔环柱形、3孔柱形以及5孔柱形颗粒床层模型,分析反应器床层孔隙率、速度场和压力场的变化。结果表明,不同形状颗粒床层的流场均匀度从高到低的顺序为柱形、3孔柱形、5孔柱形、大孔环柱形和小孔环柱形,柱形颗粒床层主流道径向压差最高,床层孔隙率最低,床层径向速度及压降沿轴向变化最小,流体分布最均匀。     

最小?损优化方法在椭圆换热管内的应用

在流体对流换热分析的基础上得到局部?损率的表达式,以局部?损率为优化目标,满足能量与质量守恒条件,在流动功耗为定值条件下,根据拉格朗日泛函极值原理得到?损为极值时的控制方程组,发展了最小?损优化方法。将该方法应用到椭圆换热单管中,得到优化后的速度场与温度场。优化结果表明,优化流动结构为纵向旋流,具有较好的传热及流动性能,相比未优化椭圆管综合换热性能（Nu/Nu_s）/（f/f_s）可达3.21,同时得到了纵向涡在流场中的分布情况,这对椭圆管内强化换热发展具有指导意义。     

基于CFD-DEM的柱形颗粒固定床反应器流场特性数值模拟

采用计算流体动力学-离散单元耦合法(CFD-DEM),研究了柱形颗粒随机堆积固定床床层的流场流动特性。建立更接近柱形催化剂实体形状的颗粒模型,采用颗粒随机堆积法建立了固定床床层,通过对床层内部的流动特性数值模拟,得到床层内部空隙分布云图及压力场和速度场的分布规律。改变管径和粒径的比值(N,简称直径比),建立N为3,5,10和20的反应器固定床床层,分析了直径比对流场特性的影响。结果表明,当N为5时,床层堆积较为密实均匀,压降较大,速率变化幅度较小,故此管径比下固定床反应器内柱状催化剂床层有较好的流场特性。     

三维整体式喷动-流化床结构优化与流动数值模拟

为了对环隙区内的颗粒堆积层产生局部流化作用,提出了一种在喷动床锥体处开一定数量侧喷嘴的整体式多喷嘴喷动-流化床结构,并采用双流体模型(TFM)对三维整体式多喷嘴喷动-流化床内的气固两相流动行为进行了数值模拟。通过计算流体力学(CFD)模拟获得了喷动床内颗粒体积分数、颗粒速度及流场均匀度分布情况,并将模拟结果与传统喷动床进行了对比,同时对锥体处开孔直径等关键参数进行了优化分析。结果表明:与常规喷动床相比,三维整体式多喷嘴喷动-流化床结构能有效增强喷动床环隙区与喷射区颗粒的径向混合,特别是流化了喷动床环隙区底部颗粒的流动死区。颗粒流场均匀度(CV)值随着床层高度的增加而上升,表明多喷嘴对颗粒流场的均匀化效应主要体现在喷动床柱锥区,当A_i/A_z=0.67时,侧喷嘴对喷动-流化床内整体的颗粒流化作用达到最佳。     

单一尺寸圆柱颗粒填充床的阻力特性

通过直径为3、4 mm不同长度的圆柱颗粒填充床的阻力特性实验,研究了颗粒密度对填充床孔隙率的影响,结合文献孔隙率数据修正了孔隙率模型使其在高球形度时预测更准,分析了等效直径的计算方法对Ergun常数的影响,得到圆柱颗粒填充床的阻力特性并与Nemec和Wu的阻力预测模型进行对比,提出新的拟合方法对Ergun常数进行拟合。结果表明:颗粒密度在1156～7947 kg/m~3范围内对填充床的孔隙率没有影响;结合文献数据得到圆柱颗粒填充床的孔隙率修正模型;文献中预测不同L/D的圆柱颗粒堆积床的阻力时结果相差较大,Nemec模型要比Wu模型预测准确度高,但也不适用所有L/D下的阻力预测;结合圆柱颗粒填充床孔隙率提出新的拟合方法,拟合Ergun常数时,采用dep作为等效直径的拟合优度最高;提出新的Ergun常数表达式,适用于圆柱直径3～4 mm,L/D=1～10的圆柱颗粒,相比于Nemec模型其R~2更高,适用范围更明确,因此实用性更强。     

烯烃催化裂解反应器局部颗粒堆积结构的颗粒解析模拟

烯烃催化裂解固定床工艺中的反应过程对压力敏感,深入研究催化剂堆积颗粒结构中的流动及压力分布对优化固定床结构及操作参数有重要意义。颗粒解析模拟方法广泛用于固定床内堆积结构的模拟,可以准确描述堆积结构中的流体力学行为,但对于复杂堆积结构网格生成困难。采用基于多孔介质模型的浸入边界法(PMM-IBM)结合网格自适应,实现了对固定床堆积结构的颗粒解析模拟,既解决了网格划分困难的问题,又节省了计算资源。采用网格自适应技术后,与均匀网格相比,堆积结构的网格总数减少大约80%。通过与贴体网格法的单颗粒表面受力分析对比,确定了此浸入边界法的关键模拟参数。随后模拟预测了三种床层与颗粒直径比值条件下堆积结构的空隙率及其内部的压力及流动分布。研究表明,堆积结构空隙中的局部轴向速度的最大值可以达到入口速度的10倍以上,轴向平均速度的径向分布与轴向平均空隙率分布一致,均成震荡衰减趋势。除此之外,预测的床层压降与Reichelt经验关联式结果较为吻合。在此基础上,耦合单颗粒内扩散和烯烃裂解的主反应,预测了反应物随孔径和孔隙率的变化,为进一步考虑外流场的变化奠定了方法基础。     

分层填料旋转床气相流场的CFD模拟研究

分层填料旋转床(SP-RPB)是一种新型高效的化工过程强化设备,对气相阻力控制的吸收、精馏等传质过程有明显的强化作用。文中采用计算流体力学方法(CFD)对该结构旋转床内的气相流场进行了模拟研究,分析了流体流速、转子转速及填料转动形式对SP-RPB内部压力场、速度场和湍动能分布的影响规律。计算使用RNG k-ε湍流模型和SIMPLE算法,填料层用多孔介质(Porous Media)模型,模拟结果与实验数据吻合良好。结果表明:SP-RPB内气相压降主要产生在填料区,切向速度远大于径向速度,流场以旋转场为主,湍动程度高于普通的旋转填料床,且湍动能沿径向的分布更为均匀,表明分层填料旋转床在强化气相传质方面比普通旋转填料床更具优势。     

Numerical determination of fluid-to-particle mass and heat transfer coefficients in packed bed reactors

A method based on particle-resolved CFD is built and validated, to calculate the fluid-to-particle mass and heat transfer coefficients in packed beds of spheres with different tube-to-particle diameter ratios (N) and of various particle shapes with N = 5.23. This method is characterized by considering axial dispersion. The mass and heat transfer coefficients increase by 5%–57% and 9%–63% after considering axial dispersion, indicating axial dispersion should be included in the method. The mass and heat transfer coefficients are reduced as N decreases. The catalyst particles without inner holes show higher mass and heat transfer coefficients than the ones with inner holes, because of unfavorable fluid flow in inner holes. The bed of trilobes has the highest mass and heat transfer coefficients, being 85% and 95% higher than the one of spheres. This work provides a versatile method and some useful guidance for the design of packed bed reactors.     

小直径比固定床壁效应的CFD分析

引言固定床作为反应器、分离器、换热器等单元设备广泛应用于化工、能源、环境等许多领域。因用途的不同固定床的管径-粒径比(D/d)的范围很宽(1～1000的数量级)。大热负荷的填充床设备,如强放热的化学反应器、核反应堆的冷却壁管列等,常采用较小的管径-粒径比,以利于热量通过     

Angular porosity distributions in fixed packed beds of low diameter aspect ratio

The angular porosity distribution for fixed packed beds of monosized spheres in cylindrical containers with low diameter aspect ratios (1 ≤ D/d ≤ 2) is determined from the spheres' center coordinates. By dividing the packed bed into a large number of identical wedge-shaped segments, the angular porosity distribution is established from the local angular porosity and the angular positions within the cylindrical container. A correlation which accurately predicts the local angular porosity is determined from the angular porosity distributions. The correlation is a function of D/d and the angular position in the cylindrical container.     

Radial porosity distribution in cylindrical beds packed with spheres

Experimental determinations of radial porosity for cylindrical beds packed with spheres are reported. The data indicate that, for a wide range of bed and sphere sizes, porosity varies significantly and regularly near the container wall. For uniformly sized spheres, the oscillations in porosity can be detected up to a distance of about 5 particle diameters from the wall. For mixtures of spheres of two sizes, regular oscillations are detected only up to 2 or 3 diameters from the wall and for three sizes the effect of the wall is observed only within a distance of 1 particle diameter.     

Flow characteristics in packed and fluidized rotating beds

Free particles in a rotating tapered cylindrical container are, as a consequence of the circular motion, forced radially outwards towards the circumference to form a packed annular bed. If the container wall is porous and a fluid is allowed to flow radially inward, the bed material may become fluidized. In the resultant centrifugal fluidized bed, radial accelerations many times one g can be generated, permitting much larger fluid flow rates during fluidization than are possible with a conventional fluidized bed. Entrainment of material can also be greatly reduced in such a geometry.The flow in both packed and fluidized beds in a rotating system is analyzed. Expressions are found for the shape of the bed as well as the distribution of particles in packed beds containing mixtures of materials having different size distributions and densities. Based on these results, equations predicting the pressure drop and radial flow distribution are deduced. The condition and location where initial fluidization of the packed bed occurs are predicted. Similarly, conditions in the fluidized state are analyzed, and it is shown that the tangential velocity distribution in the bed under these conditions is directly proportional to the bed radius.Experiments confirming the validity of the analytic models are conducted over a range of operating conditions for different bed materials.     

A radial void fraction correlation for packed bed tubes

The radial void fraction distribution of equal sized spheres in cylindrical packed bed tubes with low diameter aspect ratios (1 ≤ D/d ≤ 2) is determined from the spheres' center coordinates, the local radial void faction and the radial positions within the tubes. A correlation that closely predicts the local radial void fraction at a radial position is determined from the radial void fraction distributions. The correlation is a function of the diameter aspect ratio and the radial position in the cylindrical packed bed tubes.     

Analysis of a ring-shaped sensor for use in packed-bed heat transfer studies

A new type of ring-shaped temperature sensor for packed-bed heat transfer studies is presented. This ring-shaped sensor is easy-to-build and allows one to filter the experimental angular temperature fluctuations. This device is more effective for beds of small tube-to-particle diameter ratio. The proposed device is able to eliminate the effect of the angular position on temperature measurements in packed beds. This sensor property is confirmed both experinientally and theoretically. For demonstration purpose, packed beds of six different materials were studied. Effective thermal radial parameters obtained using the ring-shaped sensors have shown trends similar to published packed-bed heat transfer data.     

Wall to fluid heat transfer in liquid fluidised beds: Part 2

Wall to fluid heat transfer coefficients and radial temperature profiles have been obtained for beds of hydrodynamically similar spheres fluidized with water in a 2.058 inch pipe at a constant heat flux. From packed bed to open pipe conditions, heat transport occurs mainly by turbulent mixing, although conduction through the particles and possibly particle convection have some effect at low porosities. This result contradicts a previously published prediction based on model calculations using erroneous temperature profiles⁽²⁴⁾. The model predicts a minor role for particle convection when appropriate temperature profiles are used. A series model based on the observed shift of thermal resistance from the wall region to the bulk of the bed with decreasing porosity is used to correlate heat transfer coefficients. The shift in resistance largely accounts for the maximum in heat transfer coefficient plots.     

Particle-resolved simulation of packed beds by non-body conforming locally refined orthogonal hexahedral mesh

The traditional fixed-bed reactor design is usually not suitable for the low tube-to-particle diameter ratios (N=D/d < 8) where the local phenomena of channeling near the wall and backflow in the bed are dominant. The recent "solid particle" meshing method is too complicated for mesh generation, especially for non-spherical particles in large random packed beds, which seriously hinders its development. In this work, a novel high-fidelity mesh model is proposed for simulation of fixed bed reactors by combining the immersed boundary and adaptive meshing methods. This method is suitable for different shapes of particles, which ingeniously avoids handling the complex "contact point" problem. Several packed beds with two different shapes of particles are investigated with this model, and the local flow in the bed is simulated without geometrical simplification. The predicted pressure drop across the fixed bed and heat transfer of the single particle are in good agreement with the corresponding empirical relations. Compared with spherical particles, the packed bed packing with pentaphyllous particles has lower pressure drop and better heat/mass transfer performance, and it shows that this method can be used for the screening of particle shapes in a fixed bed.     

Radial porosity in packed beds of spheres

A functional approach has been developed to investigate the radial porosity of mono-sized spheres in cylinders. Analytical and semi-analytical equations have been developed to calculate the local radial porosity and the radial porosity distribution, respectively, within a cylindrical packing structure. The analytical equations are based upon fundamental principles and are simple, straightforward and provide highly accurate results for the radial porosity with minimal computational prerequisites. The analytical equations have been developed for the fixed packing of identical spheres in cylindrical containers with D/d ≥ 2.0. The predicted results for the local radial porosity and the radial porosity distributions are benchmarked with an existing analytical equation and available experimental data, respectively, for mono-sized spheres in cylindrical containers.