基于金属氢化物高温蓄热的氢热耦合传递机理

doi:10.11949/0438-1157.20210188

摘要/Abstract

摘要：

目前大多数可再生能源如太阳能具有间歇性和不稳定性的问题，因此高效蓄热技术成为了发展太阳能的一个关键途径。金属氢化物高温蓄热技术作为热化学蓄热中最有前途的方法之一，受到了人们的广泛关注。为了实现金属氢化物高温蓄热技术的工程应用，明确其氢热耦合传递机理至关重要。本研究采用数值模拟的方法，通过建立反应器的多物理场耦合模型，讨论了不同时刻下床层内部参数的分布，得到了反应锋面的形成和移动机理以及非均匀反应的形成机理；此外，结合反应器内部氢压、接触热阻和床层热阻的变化规律，明确了不同阶段下金属氢化物高温蓄热技术的控制环节；最后，依据金属氢化物高温蓄热技术的工程应用挑战，提出了相应的研究策略。

关键词: 太阳能, 金属氢化物, 高温蓄热, 传递, 反应器, 数值模拟

Abstract:

At present, most renewable energy sources such as solar energy have intermittent and unstable problems, so high efficiency heat storage technology has become a key way to develop solar energy. Metal hydride high temperature heat storage technology, as one of the most promising methods of thermochemical heat storage, has been widely concerned. To realize the engineering application of metal hydride high temperature heat storage technology, it is necessary to investigate the transfer mechanism with hydrogen thermal coupling. In this paper, a multi-physical model of the reactor was established, and the variation law of the reactor parameters was obtained. By discussing the distribution of bed temperature and reaction fraction, the heat output of the reactor was divided into three stages: initial stage, platform stage and decline stage. At the same time, taking the peak point as the boundary, the initial stage can be divided into the initial rising stage and the initial descending stage. And the formation and movement mechanism of reaction front and the formation mechanism of inhomogeneous reaction were obtained. It can be concluded that hydrogen pressure, thermal contact resistance and bed thermal resistance are the control steps of corresponding stages. In addition, the variation of reactor parameters was obtained under different hydrogen pressure, thermal contact resistance and bed thermal resistance. Through comparative analysis, it was found that hydrogen pressure was the main parameter to regulate the maximum output temperature of the reactor. Compared with the thermal contact resistance, the bed thermal resistance showed more obvious effect on the heat output of the reactor. Finally, it was pointed out that to realize the engineering application, improving the thermal conductivity of the bed was the most promising choice to enhance the performance of metal hydride high temperature heat storage system.

Key words: solar energy, metal hydride, high temperature heat storage, transport, reactors, numerical simulation

中图分类号:

TK 512⁺.4

刘洋, AYUB Iqra, 杨福胜, 吴震, 张早校. 基于金属氢化物高温蓄热的氢热耦合传递机理[J]. 化工学报, 2021, 72(9): 4607-4615.

Yang LIU, Iqra AYUB, Fusheng YANG, Zhen WU, Zaoxiao ZHANG. Hydrogen thermal coupling transfer mechanism based on metal hydride high temperature heat storage technology[J]. CIESC Journal, 2021, 72(9): 4607-4615.

图/表 14

图1 金属氢化物高温蓄热反应器几何模型

Fig.1 Geometric model of metal hydride high temperature thermal storage reactor

图2 金属氢化物高温蓄热反应模型验证

Fig.2 Model verification

图3 床层平均反应分数和换热流体输出温度随时间的变化

Fig.3 Variation curves of average bed reaction fraction and heat transfer fluid output temperature with time

图4 初始阶段不同时刻下的床层参数分布（从左至右时刻依次为7、14、21、28、36 s）

Fig.4 Distribution of bed parameters at different time of initial stage

图5 初始下降阶段不同时刻下的床层反应分数分布（从左至右时刻依次为36、80、120、160、200 s）

Fig.5 Distribution of bed reaction fraction at different time in initial descending stage

图6 平台阶段不同时刻下的床层反应分数分布(从左至右时刻依次为500、2000、4000、6000、9000 s)

Fig.6 Distribution of bed reaction fraction at different time in platform stage

图7 衰退阶段不同时刻下的床层反应分数分布(从左至右时刻依次为9000、9375、9750、10125、10500 s)

Fig.7 Distribution of bed reaction fraction at different time in decline stage

图8 衰退阶段不同时刻下的床层温度分布(从左至右时刻依次为10500、11000、12000、13000、14000 s)

Fig.8 Distribution of bed temperature at different time in decline stage

图9 不同压力下床层平均反应分数和换热流体输出温度随时间的变化曲线

Fig.9 Variation curves of average bed reaction fraction and heat transfer fluid output temperature with time under different pressures

图10 不同压力下换热流体输出峰值点参数随时间的变化规律

Fig.10 Variation law of heat transfer fluid peak point parameters with time under different pressures

图11 不同壁面传热系数下床层平均反应分数和换热流体输出温度随时间的变化

Fig.11 Variation curves of average bed reaction fraction and heat transfer fluid output temperature with time under different wall heat transfer coefficients

表1 不同壁面传热系数下峰值点参数、反应锋面参数和输出温度

Table 1 Peak point， reaction front parameters and output temperature under different wall heat transfer coefficients

壁面传热系数/ (W/(m²·K))	峰值点对应时间/s	峰值点对应温度/℃	反应锋面形成时间/s	反应锋面形成温度/℃	初始下降斜率/(℃/s)	有效输出温度/℃
1000	34.60	331.27	91.66	327.65	0.063	313.23
1500	34.60	333.87	84.71	329.84	0.080	313.67
2000	32.06	335.32	80.23	331.19	0.086	313.96
2500	32.06	336.26	76.31	332.59	0.088	314.03
3000	32.06	336.91	71.35	333.11	0.097	314.14

图12 不同床层热导率下床层平均反应分数和换热流体输出温度随时间的变化

Fig.12 Variation curves of average bed reaction fraction and heat transfer fluid output temperature with time under different bed thermal conductivity

表2 不同床层热导率下峰值点参数、反应器输出参数

Table 2 Peak point and reactor output parameters under different bed thermal conductivity

床层热导率/ (W/(m·K))	峰值点对应时间/s	峰值点对应温度/℃	有效输出温度/℃	平台末端时间/s	反应完成时间/s	300℃对应时间/s	余热散热时间/s	散热段斜率/ (℃/s)
1.0	32.06	336.91	314.14	8113.33	8901.81	11204.18	2302.37	0.0061
1.5	32.06	338.56	317.92	6156.81	7073.56	9174.89	2101.33	0.0085
2.0	34.60	339.56	322.50	5311.92	6175.61	8040.73	1865.12	0.0121
2.5	33.64	340.24	325.43	4912.98	5672.79	7306.30	1633.51	0.0156
3.0	34.78	340.73	327.11	4201.35	5324.55	6869.36	1544.81	0.0175

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