流化床液固两相传质过程的模拟研究进展

doi:10.11949/0438-1157.20210680

摘要/Abstract

摘要：

液固两相流化床具有液固相接触效率高、传质和传热性能好、颗粒分布均匀等优点，已被广泛应用于众多工业过程中。然而，流化床中与传质过程耦合的颗粒流化的复杂非线性特征及其湍动特性，使得对传质过程特性的研究十分困难。且仅依靠实验观测和理论预测难以揭示多相流相互作用规律，无法获得全面和详细的速度场和浓度场分布情况。近年来，数值模拟的快速发展为深入探索流化床中液固两相流动行为及其与传质过程耦合问题提供了重要的途径。本文对流化床液固两相流动与传质过程模拟方法进行了综述，并对其未来研究趋势进行了展望。借助于计算传质学理论可以更精确地预测局部浓度的分布情况，进而可以深入分析液固两相流化床中的传质过程规律与传质特性，为液固两相流化床的设计和优化提供理论基础。

关键词: 流化床, 两相流动, 传质过程, 数值模拟, 计算传质学, 湍流传质扩散

Abstract:

The liquid-solid two-phase fluidized bed has the advantages of high liquid-solid contact efficiency, good mass and heat transfer performance, uniform particle distribution, etc., and has been widely used in many industrial processes. However, due to the complex nonlinear characteristics and turbulent characteristics of the particle fluidization coupled with the mass transfer process in the fluidized bed, it is very difficult to study the characteristics of the mass transfer process. Moreover, it is difficult to reveal the interaction law of multiphase flow and impossible to obtain a comprehensive and detailed distribution of velocity field and concentration field only by relying on experimental observations and theoretical predictions. In recent years, the rapid development of numerical simulation has provided an important way for in-depth exploration of the liquid-solids two-phase flow behavior and its coupling with the mass transfer process in a fluidized bed. In this paper, the simulation methods of fluidized bed liquid-solids two-phase flow and mass transfer process are reviewed, and its future research trends is prospected. With the help of computational mass transfer (CMT) theory, the local concentration distribution can be predicted more accurately, and the mass transfer characteristics in the liquid-solids two-phase fluidized bed can be analyzed in depth, which provides the design and optimization of the liquid-solids two-phase fluidized bed a solid foundation.

Key words: fluidized-bed, two-phase flow, mass transfer process, numerical simulation, computational mass transfer, turbulent mass diffusion

中图分类号:

TQ 021.4

任盼锋, 海润泽, 李奇, 李文彬, 余国琮. 流化床液固两相传质过程的模拟研究进展[J]. 化工学报, 2022, 73(1): 1-17.

Panfeng REN, Runze HAI, Qi LI, Wenbin LI, Guocong YU. Review of numerical study on liquid-solids two-phase mass transfer process in fluidized bed[J]. CIESC Journal, 2022, 73(1): 1-17.

图/表 9

图1 液固两相流化床装置示意图

Fig.1 Schematic diagram of liquid-solids two-phase fluidized bed devices

图2 液固循环流化床的环-核流动结构模型示意图[27]

Fig.2 Schematic diagram of core-annular flow structure model for LSCFB[27]

图3 传递过程的数值模拟

Fig.3 Numerical simulation of transfer process

图4 液固两相流不同模拟方法

Fig.4 Different simulation methods of liquid-solids two-phase flow

图5 气固鼓泡塔中各向异性湍流传质模型[40]

Fig.5 Anisotropic turbulent mass transfer model in gas-solid bubble column[40]

表1 流化床液固两相传质系数关联式和主要参数

Table 1 Correlations and main parameters of liquid-solids mass transfer coefficients in fluidized beds

文献	颗粒直径/m	几何参数			颗粒Reynolds数(Re_p)	Schmidt数(Sc)	关联式
文献	颗粒直径/m	塔径/m	塔高/m	液含率	颗粒Reynolds数(Re_p)	Schmidt数(Sc)	关联式
[64]	0.0007~0.0024	0.051	0.6096	0.65~0.90	5~130	1020~1540	$j D = 1.340 R e p' 1 - ε l - 0.468 S h = 2 + 1.031 1 - ε l ? R e p' 0.5 S c 0.333$
[65]	0.0381	—	—	0.26~0.47	200~1230	1310~1670	$S h = 2 1 - 1 - ε l 0.333 + 0.7 ε l S c 0.333 R e p n 2 - 3 n 3 n - 1 = 4.65 R e - 0.28$
[66]	0.00027~0.00055	0.035	0.2	0.5~0.92	0.22~6.4	0.052	$S h ε l = 0.7 R e S c 0.33 ?$
[67]	0.00305~0.00635	—	—	0.49~0.94	7~7000	1~2000	$j D = 17 6 G a μ l - 1 1 - ε l 0.2, ? R e p ″ < 10 1.46 6 G a μ l - 0.41 1 - ε l 0.2, ? R e p ″ > 10$
[68]	0.0005~0.002	0.054	0.5	0.47~0.91	1~100	991~1130	$j D 1 - ε l d p 2.6 f' ? = K G d p 0.27 - 1 K = 1.15 × 10 - 10 ρ l ρ s - ρ l μ 1.33 S c 23$
[69]	0.012~0.009	0.045	—	0.50~0.90	0.0405~11610	572~1350	$j D = 1.622 ? R e p ″ - 0.444, ? R e p ″ < 20 3.815 ? R e p ″ - 0.731, ? R e p ″ > 20$
[70]	0.0046~0.0082	—	—	0.40~0.95	16~1320	305~1595	$S h = 0.254 G a 0.323 ? M v 0.3 S c 0.4$
[71]	—	0.05	1	0.80~1.0	—	—	$S h = 0.254 Φ 1.35 G a 0.323 ? M v 0.3 S c 0.4$
[72]	0.0046~0.0381	—	—	0.40~0.95	1~1320	305~1670	$S h = 1.2 0.33 d p Φ U t ρ l μ l 0.333 S c 13, ? R e t < 500 0.5 0.33 d p Φ U t ρ l μ l 0.667 S c 13, ? R e t > 500$
[73]	0.0004~0.0009	0.0508	—	0.61~0.81	0.25~22.2	368~2896	$S h = 0.65 R e t 0.468 S c 0.333$
[74]	0.0000236~0.127	—	—	0.40~0.95	0.01~1000	0.3~1755	$ε l j D = 1.1068 R e - 0.72, ? R e p < 10 0.455 R e - 0.407, ? R e p > 10$
[75]	0.0004~0.001	0.051	—	0.55~0.85	2~25	336~451	$S h = 0.86 ε l R e p 0.5 S c 0.333$
[76]	0.0003~0.0008	—	—	0.54~0.65	0.644~7.312	998~1316	$j D = 1.489 ? R e p' - 0.4506 k s l = 3.22 × 10 - 5 U l 0.272 d p - 0.04$
[77]	0.000614	0.039	0.6	0.7~0.9	5~8	470	$S h = 7.55 ε l - 1 R e m - 0.6 S c 0.33$
[78]	0.021	0.04	—	0.41~0.46		969	$ε l j D = 0.64 R e - 0.6 1 - ε l 0.4$
[79]	0.0049~0.0061	0.192	0.6	0.50~0.70	112~288	970	$S h = 5.4 × 10 - 2 ε l 2 R e S c 0.33$
[80]	0.0064~0.0082	0.094	2	0.70~0.95	590~2120	1~1.06	$S h = 0.763 ε l - 1.20 R e 0.556 S c 0.333, ? ε l < 0.815 0.268 ε l - 2.40 R e 0.669 S c 0.333, ? ε l > 0.815$
[81]	—	—	—	0.53~0.96	180~1320	300~2000	$S h = 0.215 R e 0.011 G a 0.309 M v 0.303 S c 0.436, ? ε l < 0.815 0.115 R e - 0.076 G a 0.390 M v 0.503 S c 0.436, ? ε l > 0.815$

表1 流化床液固两相传质系数关联式和主要参数

Table 1 Correlations and main parameters of liquid-solids mass transfer coefficients in fluidized beds

文献	颗粒直径/m	几何参数			颗粒Reynolds数(Re_p)	Schmidt数(Sc)	关联式
文献	颗粒直径/m	塔径/m	塔高/m	液含率	颗粒Reynolds数(Re_p)	Schmidt数(Sc)	关联式
[64]	0.0007~0.0024	0.051	0.6096	0.65~0.90	5~130	1020~1540	$j D = 1.340 R e p' 1 - ε l - 0.468 S h = 2 + 1.031 1 - ε l ? R e p' 0.5 S c 0.333$
[65]	0.0381	—	—	0.26~0.47	200~1230	1310~1670	$S h = 2 1 - 1 - ε l 0.333 + 0.7 ε l S c 0.333 R e p n 2 - 3 n 3 n - 1 = 4.65 R e - 0.28$
[66]	0.00027~0.00055	0.035	0.2	0.5~0.92	0.22~6.4	0.052	$S h ε l = 0.7 R e S c 0.33 ?$
[67]	0.00305~0.00635	—	—	0.49~0.94	7~7000	1~2000	$j D = 17 6 G a μ l - 1 1 - ε l 0.2, ? R e p ″ < 10 1.46 6 G a μ l - 0.41 1 - ε l 0.2, ? R e p ″ > 10$
[68]	0.0005~0.002	0.054	0.5	0.47~0.91	1~100	991~1130	$j D 1 - ε l d p 2.6 f' ? = K G d p 0.27 - 1 K = 1.15 × 10 - 10 ρ l ρ s - ρ l μ 1.33 S c 23$
[69]	0.012~0.009	0.045	—	0.50~0.90	0.0405~11610	572~1350	$j D = 1.622 ? R e p ″ - 0.444, ? R e p ″ < 20 3.815 ? R e p ″ - 0.731, ? R e p ″ > 20$
[70]	0.0046~0.0082	—	—	0.40~0.95	16~1320	305~1595	$S h = 0.254 G a 0.323 ? M v 0.3 S c 0.4$
[71]	—	0.05	1	0.80~1.0	—	—	$S h = 0.254 Φ 1.35 G a 0.323 ? M v 0.3 S c 0.4$
[72]	0.0046~0.0381	—	—	0.40~0.95	1~1320	305~1670	$S h = 1.2 0.33 d p Φ U t ρ l μ l 0.333 S c 13, ? R e t < 500 0.5 0.33 d p Φ U t ρ l μ l 0.667 S c 13, ? R e t > 500$
[73]	0.0004~0.0009	0.0508	—	0.61~0.81	0.25~22.2	368~2896	$S h = 0.65 R e t 0.468 S c 0.333$
[74]	0.0000236~0.127	—	—	0.40~0.95	0.01~1000	0.3~1755	$ε l j D = 1.1068 R e - 0.72, ? R e p < 10 0.455 R e - 0.407, ? R e p > 10$
[75]	0.0004~0.001	0.051	—	0.55~0.85	2~25	336~451	$S h = 0.86 ε l R e p 0.5 S c 0.333$
[76]	0.0003~0.0008	—	—	0.54~0.65	0.644~7.312	998~1316	$j D = 1.489 ? R e p' - 0.4506 k s l = 3.22 × 10 - 5 U l 0.272 d p - 0.04$
[77]	0.000614	0.039	0.6	0.7~0.9	5~8	470	$S h = 7.55 ε l - 1 R e m - 0.6 S c 0.33$
[78]	0.021	0.04	—	0.41~0.46		969	$ε l j D = 0.64 R e - 0.6 1 - ε l 0.4$
[79]	0.0049~0.0061	0.192	0.6	0.50~0.70	112~288	970	$S h = 5.4 × 10 - 2 ε l 2 R e S c 0.33$
[80]	0.0064~0.0082	0.094	2	0.70~0.95	590~2120	1~1.06	$S h = 0.763 ε l - 1.20 R e 0.556 S c 0.333, ? ε l < 0.815 0.268 ε l - 2.40 R e 0.669 S c 0.333, ? ε l > 0.815$
[81]	—	—	—	0.53~0.96	180~1320	300~2000	$S h = 0.215 R e 0.011 G a 0.309 M v 0.303 S c 0.436, ? ε l < 0.815 0.115 R e - 0.076 G a 0.390 M v 0.503 S c 0.436, ? ε l > 0.815$

表2 流化床液固两相流动行为模拟

Table 2 Simulation of liquid-solids two-phase flow in fluidized beds

文献	颗粒密度/ (kg/m³)	颗粒直径/mm	模拟对象				表观液速/(m/s)	曳力模型	多相流模型
文献	颗粒密度/ (kg/m³)	颗粒直径/mm	装置	塔径/m	塔高/m	液含率	表观液速/(m/s)	曳力模型	多相流模型
[82]	2490	0.508	LSCFB riser	0.076	3.0	0.94~1	0.12~0.35	Wen-Yu	E-E
[83]	2540	1.13	LSFB	0.127	1.1	0.6~1	0.0085~0.110	Wen-Yu, Gidaspow	E-E
[84]	1075~2803	0.8~3.0	LSFB	0.1	1.2	0.7~1	0.003~0.0012	Pandit-Joshi	E-E
[85]	3000	25	LSFB	0.1	0.5	0.44~1	0.03~0.14	Syamlal O’Brien	E-E
[86]	2500	0.3	LSFB	0.14	1.5	0.37~1	0.025	Beetstra et al., Wen-Yu, Gidaspow	E-E
[87]	2173	0.75~0.93	LSFB	0.1	1.8	0.7~1	0.031~0.093	Wen-Yu, Gidaspow, Ergun, Gibilaro, Swamee-Ohja, Haider-Levenspiel, Schiller-Naumann, Syamlal O’Brien	E-E
[88]	2500	3	LSFB	0.14	0.5	0.5~1	0.07~0.13	Gidaspow	E-L
[89]	2540	1.13	LSFB	0.14	0.5	0.5~1	0.0085~0.110	Gibilaro	E-E
[90]	2500	0.508	LSCFB riser	0.0762	3	0.8~1	0.0075	EMMS	E-E
[91]	8710	6~8	LSFB	0.05	1.5	0.4~1	0.06~0.22	—	E-E, E-L
[92]	897	2	inverse LSFB	0.5	1.5	0.45~1	0.009~0.025	Gidaspow	E-E
[93]	1080	0.32	LSCFB downer	0.06	3	0.6~1	0.0055	Wen-Yu	E-E
[94]	2540~7780	2.06~6	LSFB	0.512	2.04	0.45~1	0.04~0.1	Huilin-Gidaspow	E-L
[95]	1050~8000, 25~950	0.8~3	UCFB, DCFB	0.076, 0.2	5.4	0.89~1	0.12~0.53	Syamlal O’Brien	E-E
[96]	2460	0.9~1	cuboid LSFB	0.3×0.025	1	0.5~1	0.025~0.054	Wen-Yu, Dallavalle, TGS, Gidaspow, Syamlal O’Brien	E-E
[53]	1080	0.32	LSCFB riser	0.038	3	0.98~1	0.0113~0.0187	Gidaspow	E-E
[51]	1200~1800	0.135~0.2	LSFB	0.05	1	0.8~1	0.0003~0.0014	Wen-Yu, Syamlal O’Brien, Gibilaro, Gidaspow	E-E
[52]	2490	0.508	LSCFB riser	0.076	3	0.98~1	0.15	Gidaspow	E-E

图6 示踪剂扩散过程模拟结果[53]

Fig.6 Simulation results of tracer diffusion process[53]

图7 流动行为耦合传质过程的CFD模拟结果[51]

Fig.7 CFD simulation results of flow behavior coupling mass transfer process[51]

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