双流化床化学链制氢反应器的数值模拟

doi:10.11949/0438-1157.20240220

摘要/Abstract

摘要：

化学链制氢技术具有能耗低、产氢纯度高、清洁高效等优势，在氢能领域越来越受到重视。化学链制氢系统中复杂的流动与传递过程限制了该技术的发展，需要开展深入的研究工作揭示化学链制氢反应器的运行特性。使用双流体模型对化学链制氢双流化床反应器进行三维数值模拟研究，考察不同操作工况和载氧体属性对系统运行的影响，揭示反应器内部压力和固相浓度分布规律，为双流化床化学链制氢装置的运行和优化提供指导。计算结果表明，随着床料量增加，提升管压力波动幅值减小，运行更加平稳；由于进料口布置形式的影响，在提升管入口段固相分布呈现较强的不对称性；当前工况下提升管入口气速为7 m/s时反应器运行最平稳，随着流化气速增加固体循环量出现剧烈波动。

关键词: 化学链制氢, 载氧体, 循环流化床, 多相流, 计算流体力学

Abstract:

Chemical looping hydrogen generation technology has the advantages of low energy consumption, high purity of hydrogen production, cleanness and efficiency, etc., and is receiving more and more attention in the field of hydrogen energy. However, the complex flow and mass transfer mechanisms inherent in the system pose significant challenges to its technological development. Therefore, conducting comprehensive research aimed at elucidating the operational characteristics of the chemical looping hydrogen generation reactor is of significant importance. This study performs a three-dimensional numerical simulation of a dual fluidized bed reactor for chemical looping hydrogen generation utilizing the two-fluid model (TFM) to examine the impacts of various operating conditions and oxygen carrier properties on system performance. The particle quantity and pressure drop in the riser obtained from the simulation agree well with experimental results, which suggests that the current model is capable for the simulation. The numerical results show that increasing the bed material reduces the pressure fluctuation amplitudes in the riser, leading to enhanced operational stability. The distribution of the solid phase in the radial direction of the riser is non-uniform, attributed to the arrangement of the inlet. And non-uniformity distribution of solid becomes more pronounced at higher gas velocities and results in severe operating conditions. Under the current operating conditions, the reactor operates most steadily when the inlet gas velocity of the riser is 7 m/s, and an increase in fluidization gas velocity leads to a significant fluctuation in solid circulation. The flow characteristics of reactor, derived from numerical simulation, provide insights into the operation and optimization of the dual fluidized bed in chemical looping hydrogen generation.

Key words: chemical looping hydrogen generation, oxygen carrier, circulating fluidized bed, multiphase flow, computational fluid dynamics

中图分类号:

TQ 028.8

曹佳蕾, 孙立岩, 曾德望, 尹凡, 高子翔, 肖睿. 双流化床化学链制氢反应器的数值模拟[J]. 化工学报, 2024, 75(8): 2865-2874.

Jialei CAO, Liyan SUN, Dewang ZENG, Fan YIN, Zixiang GAO, Rui XIAO. Numerical simulation of chemical looping hydrogen generation with dual fluidized bed reactors[J]. CIESC Journal, 2024, 75(8): 2865-2874.

图/表 16

图1 化学链制氢系统示意图

Fig.1 Schematic of chemical looping hydrogen generation system

图2 双流化床化学链制氢反应器

Fig.2 Photograph and schematic structure of chemical looping hydrogen generation with dual fluidized bed reactor

表1 数值模拟工况

Table 1 Simulation conditions

模拟工况	u_ri/(m/s)	u_sp/(m/s)	u₁/(m/s)	u₂/(m/s)	颗粒总质量/kg
1	7	0.2	0.4	0.8	20.8
2	7	0.2	0.4	0.8	30.9
3	5	0.2	0.4	0.8	30.9
4	9	0.2	0.4	0.8	30.9
5	7	4	0.1	0.2	30.9
6	7	4	0.1	0.2	40.9^①

表2 数值模型参数设置

Table 2 Numerical model parameter settings

名称	参数
湍流模型	standard k-ε
颗粒碰撞恢复系数	0.9
颗粒黏度	gidaspow
固相压力	lun-et-al
颗粒体积黏度	lun-et-al
摩擦黏度	schaeffer
摩擦压力	based-ktgf
径向分布函数	lun-et-al
堆积极限	0.63

图3 反应器瞬时固相体积分数分布

Fig.3 Instantaneous solid volume fraction distribution in reactor

图4 提升管中不同高度固相体积分数分布（t=30 s）

Fig.4 Solid volume fraction distribution at different heights of the riser

图5 不同高度提升管瞬时压力

Fig.5 Profile of instantaneous gas phase pressure at different heights of riser

图6 不同高度提升管压降变化

Fig.6 Profile of pressure drop in the riser along the height

图7 提升管固相质量变化

Fig.7 Profile of instantaneous solid inventory in the riser

图8 不同气速提升管固体体积分数横向分布

Fig.8 Profile of horizontal distribution of solid volume fraction in the riser at different gas velocity

图9 不同气速提升管固相质量流量变化

Fig.9 Profile of instantaneous solid mass flow rate of the riser at different gas velocity

图10 不同气速下的固相质量分布

Fig.10 Profile of solid inventory at different gas velocity

图11 提升管1.5 m处固体体积分数横向分布

Fig.11 Profile of horizontal distribution of solid volume fraction at 1.5 m of the riser

图12 提升管1.5 m处的固相轴向速度横向分布

Fig.12 Profile of horizontal distribution of solid axial velocity at 1.5 m of the riser

图13 提升管内固相质量流量变化

Fig.13 Profile of instantaneous solid mass flow rate of the riser

图14 提升管内固相质量变化

Fig.14 Profile of instantaneous solid inventory in the riser

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