中试规模环形折流板脉冲萃取柱内液—液两相流数值模拟研究

doi:10.11949/0438-1157.20250440

摘要/Abstract

摘要：

脉冲萃取柱是乏燃料后处理过程中重要的液-液萃取设备。本文利用计算流体力学（CFD）方法对中试规模环形折流板脉冲萃取柱（APDDC）内的水力学性能进行了模拟与研究。首先，针对有机相连续和水相连续两种不同工艺过程中分散相对折流板的浸润性差异，发展了近板区等效液滴尺寸模型，分别建立了适用于两种工艺流程的欧拉—欧拉两相流模拟方法，模拟结果与实验测量结果符合良好。而后，对萃取柱内的流场、分散相分布以及分散相返混情况进行了研究，并建立了分散相板上富集度和返流率的关联式。

关键词: 萃取, 计算流体力学, 水力学性能, 两相流, 分散相分布, 模型

Abstract:

The pulsed disc and doughnut extraction column serves as a critical apparatus within spent nuclear fuel reprocessing. In this study, hydrodynamic behavior within the pilot- plant scale annular pulsed disc and doughnut extraction column was investigated via CFD. To address the differences in wettability of the dispersed phase towards plates between continuous organic phase and continuous aqueous phase processes, an equivalent droplet size model for the near-plate region was developed. Corresponding Euler-Euler two-phase flow simulation methods were established for the two different processes. The simulation results are in good accordance with the experimental results. The flow field within the extraction column, the distribution of the dispersed phase, and the backmixing of the dispersed phase were then investigated. Based on the simulation results, correlations for the enrichment degree on the plate and the backflow ratio of the dispersed phase were established.

Key words: extraction, computational fluid dynamics, hydrodynamic performance, two phase flow, distribution of dispersed phase, correlation

中图分类号:

TQ028.4

兰文杰, 景山, 袁俊涛, 李少伟. 中试规模环形折流板脉冲萃取柱内液—液两相流数值模拟研究[J]. 化工学报, DOI: 10.11949/0438-1157.20250440.

Wenjie LAN, Shan JING, Juntao YUAN, Shaowei LI. Simulation of liquid-liquid two-phase flow in a pilot-plant scale annular pulsed disc and doughnut extraction column[J]. CIESC Journal, DOI: 10.11949/0438-1157.20250440.

图/表 17

表1 体系物性参数

Table 1 Physical properties of the systems

溶液

硝酸浓度

(mol/L)

图1 环形折流板脉冲萃取柱几何结构示意图

Fig. 1 The schematic of APDDCs

表2 环形折流板脉冲萃取柱的几何结构参数

Table 2 Geometric parameters of APDDCs

编号	柱径D (mm)	环隙宽度L (mm)	圆盘直径D_d (mm)	圆环内径D_a (mm)	板间距h (mm)
C1	175	50	158	107	38
C2	215	70	192	122	48
C3	255	90	227	139	58

图2 环形折流板脉冲萃取柱计算域

Fig. 2 Calculation domain of APDDC.

图3 有机相连续工艺过程中欧拉-欧拉两相流计算模型的边界条件

Fig. 3 Boundary conditions for Euler-Euler two-phase flow calculation model under continuous organic phase process

表3 不同网格密度条件下的存留分数模拟结果

Table 3 Simulation results of volume fraction under different mesh density conditions

方法	网格尺寸	计算域总网格数	分散相存留分数
模拟计算	2.5 mm	39080	0.122
模拟计算	2 mm	75296	0.121
模拟计算	1.5 mm	153719	0.122
实验	/	/	0.12

图4 有机相连续工艺过程中的分散相存留分数模拟与实验结果对比

Fig. 4 Comparison of holdup results between experiments and simulations in continuous organic phase process

图5 有机相连续工艺过程中分散相体积分数分布注:(C1柱, F = 250 L/(dm2·h), Ra = 0.63, Af = 9.4 mm/s,以达到稳态后某一脉冲周期的起始时间为0 s)

Fig. 5 Distribution of dispersed phase volume fraction in continuous organic phase process.(Column C1, F = 250 L/(dm2·h), Ra = 0.63, Af = 9.4 mm/s. The starting time of a certain pulse period is set as 0 s after the steady state is reached.)

图6 近板区等效液滴尺寸算法下，有机相连续工艺过程中分散相存留分数模拟与实验结果对比

Fig. 6 Comparison of the simulated and experimental holdup in continuous organic phase process when the equivalent droplet size is applied in the near plate area.

图7 水相连续工艺过程中分散相存留分数模拟与实验结果对比

Fig. 7 Comparison of the simulated and experimental holdup in continuous aqueous phase process.

图8 有机相连续工艺过程中一个脉冲周期内萃取柱中的分散相体积分数分布和连续相流速分布注:(C1柱, F = 250 L/(dm2·h), Ra = 0.63, Af = 9.4 mm/s,以达到稳态后某一脉冲周期的起始时间为0 s)

Fig. 8 Dispersed phase volume fraction profile and continuous phase velocity vector in one pulsation cycle in continuous organic phase process. (Column C1, F = 250 L/(dm2·h), Ra = 0.63, Af = 9.4 mm/s. The starting time of a certain pulse period is set as 0 s after the steady state is reached.)

图9 水相连续工艺过程中一个脉冲周期内萃取柱中的分散相体积分数分布和连续相流速分布注:(C1柱, F = 250 L/(dm2·h), Ra = 0.91, Af = 7 mm/s,以达到稳态后某一脉冲周期的起始时间为0 s)

Fig. 9 Dispersed phase volume fraction profile and continuous phase velocity vector in one pulsation cycle in continuous aqueous phase process. (Column C1, F = 250 L/(dm2·h), Ra = 0.91, Af = 7 mm/s. The starting time of a certain pulse period is set as 0 s after the steady state is reached.)

图10 脉冲强度对分散相体积分数分布和连续相流速的影响（有机相连续工艺过程, C1柱, F = 250 L/(dm2·h), Ra = 0.63，以达到稳态后某一脉冲周期的起始时间为0 s）

Fig. 10 The influence of pulsation intensity on the dispersed phase volume fraction profile and continuous phase velocity （Continuous organic phase process, Column C1, F = 250 L/(dm2·h), Ra = 0.63. The starting time of a certain pulse period is set as 0 s after the steady state is reached.）

图11 总通量和流比对分散相体积分数分布和连续相流速的影响（以达到稳态后某一脉冲周期的起始时间为0 s）

Fig. 11 The influence of total flow throughput and flow ratio on the dispersed phase volume fraction profile and continuous phase velocity. （The starting time of a certain pulse period is set as 0 s after the steady state is reached.）

图12 不同因素对φ的影响

Fig. 12 The effect of different factors on φ

图13 不同工艺过程中的分散相板上富集度

Fig. 13 The degree of enrichment of the dispersed phase on the plate in two different processes

图14 分散相通量Ud的变化和返流率的预测

Fig. 14 The variation of Ud and the prediction of β

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