多孔板鼓泡塔流动与传质特性数值模拟

doi:10.11949/0438-1157.20231331

摘要/Abstract

摘要：

采用Euler-Euler双流体模型对安装不同数量的水平多孔板的鼓泡塔内气液两相流动及传质特性进行数值模拟研究，并探究了不同表观气速条件对鼓泡塔内气含率、气泡直径分布和气液传质系数的影响。结果表明，不同数量的多孔板和不同位置的多孔板都会影响气含率的分布；随着多孔板的数目增加，鼓泡塔液相上方区域的气含率增加，但影响区域有限；安装多孔板后，鼓泡塔内径向位置的平均气含率变化明显，出现“M”形状的分布。不同表观气速下，未安装多孔板的鼓泡塔内直径为1~2 mm的微小气泡占比超过30%；安装多孔板后，微小气泡占比明显增加；气液传质系数在中心区域(径向无量纲为-0.5~0.5)较为平缓，波动不大。最后将模拟计算得到的气液体积传质系数与Akita的关联式计算值进行比较，本文计算结果略高。

关键词: 鼓泡塔, CFD-PBM模型, 气泡直径, 气含率, 气液体积传质系数

Abstract:

A numerical simulation investigation was performed on the gas-liquid two-phase flow and gas-liquid mass transfer characteristics within a bubbling column reactor with various numbers of horizontally placed porous plates using the Euler-Euler dual-fluid model. Furthermore, the research investigated the impact of horizontal porous plates situated at different positions and various superficial gas velocities on gas holdup, bubble diameter, and gas-liquid mass transfer coefficient in the bubbling column reactor. The results indicate that the distribution of gas holdup was affected by the quantity and location of the porous plates. As the number of porous plates increased, the gas holdup in the upper part of the liquid phase of the bubbling column reactor increased; after installing the porous plate, the average gas holdup at the inner diameter of the reactor changed significantly, resulting in an M-shaped distribution; at various superficial gas velocities, the proportion of small bubbles with a diameter of 1—2 mm accounted for over 30% in the bubbling column reactor without the installation of a porous plate. Conversely, the proportion of small bubbles increased significantly after the installation of a porous plate. The gas-liquid mass transfer coefficient is relatively gentle in the central area (radial dimensionless between -0.5 and 0.5), with little fluctuation. Finally, the volume mass transfer coefficient obtained from the simulation calculation was compared with the calculated value of Akita’s correlation equation. The calculation result was slightly higher.

Key words: bubbling column reactor, CFD-PBM model, bubble diameter, gas holdup, gas-liquid volumetric mass transfer coefficient

中图分类号:

TQ 052.4

王娟, 李秀明, 邵炜涛, 丁续, 霍莹, 付连超, 白云宇, 李迪. 多孔板鼓泡塔流动与传质特性数值模拟[J]. 化工学报, 2024, 75(3): 801-814.

Juan WANG, Xiuming LI, Weitao SHAO, Xu DING, Ying HUO, Lianchao FU, Yunyu BAI, Di LI. Numerical simulation of flow and mass transfer characteristics in porous plate bubbling column reactor[J]. CIESC Journal, 2024, 75(3): 801-814.

图/表 18

图1 鼓泡塔CFD-PBM耦合模型计算流程图

Fig.1 Calculation flow chart of gas-liquid mass transfer CFD-PBM coupling model

图2 鼓泡塔三维结构与网格划分

Fig.2 Three-dimensional structure and grid structure of bubbling columns reactor

表1 模型建立数据汇总

Table 1 Model establishment data summary

Parameter	Value
D/mm	149
H/mm	1616
H₁/mm	160
H₂/mm	420
H₃/mm	680
H₄/mm	940
H₅/mm	1130
H₆/mm	8

图3 安装不同数量多孔板的鼓泡塔三维结构

Fig.3 Three-dimensional structure of bubbling column reactors with different numbers of porous plates installed

图4 不同数量网格下不同截面平均气含率

Fig.4 Average gas holdup of different sections under different number of grids

图5 H/D=4截面气含率模拟结果与实验结果对比

Fig.5 Comparison between simulated and experimental results of gas holdup at H/D=4 cross-section

表2 氧气与水的物性参数

Table 2 Physical parameters of oxygen and water

Object	Density/(kg/m³)	Viscosity/(Pa·s)
water	1000	0.00178
oxygen	1.492	0.000019

图6 安装不同数量多孔板的鼓泡塔纵截面气含率分布

Fig.6 Distribution of gas holdup in longitudinal section of perforated plates bubbling column reactors with different numbers

图7 安装不同数量多孔板鼓泡塔平均气含率沿径向分布

Fig.7 Radial distribution of average gas holdup in porous plates bubbling column reactors with different numbers installed

图8 安装不同数量多孔板鼓泡塔内液相流线

Fig.8 Liquid phase flow lines in porous plates bubbling column reactors with different numbers installed

图9 不同表观气速下安装4块多孔板的鼓泡塔内气泡尺寸分布情况

Fig.9 Bubble size distribution in four porous plates bubbling column reactors installed at different superficial gas velocities

图10 不同表观气速和安装不同数量多孔板的鼓泡塔内气泡直径概率密度分布

Fig.10 Probability density distribution of bubble diameter in bubbling column reactors with different superficial gas velocities and different number of perforated plates

图11 表观气速0.25 m/s时不同向多孔板数量下鼓泡塔内平均气泡直径概率径分布

Fig.11 Probability radial distribution function of average bubble diameter in the bubbling column reactors with different number of perforated plates at the superficial gas velocity of 0.25 m/s

图12 不同径向位置和表观气体速度下的气泡大小概率密度分布

Fig.12 Probability density distribution of bubble size at different radial positions and superficial gas velocities

图13 ug=0.25 m/s时安装不同位置的多孔板鼓泡塔内气泡直径分布情况

Fig.13 Distribution of bubble diameter in porous plates bubbling column reactors installed at different positions at ug=0.25 m/s

图14 不同表观气速与安装不同数量多孔板下鼓泡塔内H/D=4截面处气液界面面积

Fig.14 The gas-liquid interface area at the H/D=4 cross-section in the bubbling column reactor under different superficial gas velocities and installation of different numbers of porous plates

图15 不同表观气速与安装不同数量多孔板下鼓泡塔内平均气液传质系数径向分布

Fig.15 Radial distribution function of average gas-liquid mass transfer coefficient in bubbling column reactors with different superficial gas velocities and different number of perforated plates

图16 气液体积传质系数随表观气速变化分布

Fig.16 Distribution of gas-liquid volumetric mass transfer coefficient with superficial gas velocity

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