Numerical Study of Convective Heat Transfer Characteristics of Superheated Steam in Rod Bundle Channels at Low Reynolds Numbers
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摘要: 由于现有经验关联式及相关研究成果缺乏可靠的棒束通道内低雷诺数过热蒸汽流动与传热预测关联式，通过以棒束通道内低雷诺数（Rein=1937.90~9471.24）过热蒸汽为研究对象，采用数值模拟方法，基于大涡模拟（LES）湍流模型，探究入口蒸汽速度、过热度、初始壁面温度、出口蒸汽压力以及栅径比对棒束通道内低雷诺数过热蒸汽对流换热特性的影响，进而对现有的经验关联式进行修正。数值模拟结果表明：入口蒸汽速度、过热度、初始壁面温度、出口蒸汽压力以及栅径比的增大均会使对流换热系数增大；随着入口蒸汽速度、出口蒸汽压力以及栅径比的增大，努塞尔数增大；随着入口蒸汽过热度以及初始壁面温度的升高，努塞尔数减小。修正后的Dittus-Boelter经验关联式误差在10%以内，为指导工程实际应用以及保证压水堆堆芯安全提供了依据。Abstract: Due to the lack of reliable empirical correlations and related research results for predicting the flow and heat transfer of superheated steam in rod bundle channels at low Reynolds numbers, numerical simulation method is used to study superheated steam in rod bundle channels at low Reynolds numbers (Rein=1937.90~9471.24). This method is based on the Large Eddy Simulation (LES) turbulence model to investigate the effects of inlet steam velocity, degree of superheat, initial wall temperature, outlet steam pressure, and grid diameter ratio on the convective heat transfer characteristics of superheated steam in rod bundle channels at low Reynolds numbers, and to further modify the current empirical correlations. The numerical simulation results showed that the increase in inlet steam velocity, degree of superheat, initial wall temperature, outlet steam pressure, and grid diameter ratio all increased the convective heat transfer coefficient. As the inlet steam velocity, outlet steam pressure, and grid diameter ratio increased, the Nusselt number increased. As the inlet steam degree of superheat and initial wall temperature increased, the Nusselt number decreased. The error of the modified Dittus-Boelter empirical correlation was within 10%, providing a basis for guiding practical engineering applications and ensuring the safety of pressurized water reactor cores.
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图 1 1/4模型（栅径比1.33）三维结构示意图
Figure 1. Three-dimensional Structure Schematic Diagram of the 1/4 Model with a Grid Diameter Ratio of 1.33
图 2 1/4棒束通道横截面网格示意图
Figure 2. Schematic Diagram of the 1/4 Rod Bundle Channel Cross-Section Mesh
图 3 各组网格的包壳平均壁面温度变化趋势
Figure 3. Variation Trends of the Average Cladding Wall Temperature for Each Mesh Group
图 4 不同时间步长的包壳平均壁面温度变化趋势
Figure 4. Variation Trends of the Average Cladding Wall Temperature for Different Time Steps
图 5 LES模拟结果与FLECHT实验结果对比
Pr—普朗特数。
Figure 5. Comparison of Large Eddy Simulation (LES) Results with FLECHT Experiment Results
图 6 不同入口蒸汽速度下包壳平均热流密度变化趋势
Figure 6. Variation Trends of the Average Heat Flux of Cladding under Different Inlet Steam Velocities
图 7 不同入口蒸汽速度下包壳平均壁面温度变化趋势
Figure 7. Variation Trends of the Average Cladding Wall Temperature under Different Inlet Steam Velocities
图 8 不同入口蒸汽速度下蒸汽平均温度变化趋势
Figure 8. Variation Trends of the Average Steam Temperature under Different Inlet Steam Velocities
图 9 不同入口蒸汽速度下平均对流换热系数变化趋势
Figure 9. Variation Trends of the Average Convective Heat Transfer Coefficient under Different Inlet Steam Velocities
图 10 不同入口蒸汽速度下时均雷诺数、时均努塞尔数变化趋势
Figure 10. Variation Trends of Time-averaged Reynolds Number and Time-averaged Nusselt Number under Different Inlet Steam Velocities
图 11 不同入口蒸汽过热度下包壳平均热流密度变化趋势
Figure 11. Variation Trends of Average Heat Flux of Cladding under Different Inlet Steam Superheat Degrees
图 12 不同入口蒸汽过热度下包壳平均壁面温度变化趋势
Figure 12. Variation Trends of Average Cladding Wall Temperature under Different Inlet Steam Superheat Degrees
图 13 不同入口蒸汽过热度下平均对流换热系数变化趋势
Figure 13. Variation Trends of Average Convective Heat Transfer Coefficient under Different Inlet Steam Superheat Degrees
图 14 不同入口蒸汽过热度下时均雷诺数、时均努塞尔数变化趋势
Figure 14. Variation Trends of Time-averaged Reynolds Number and Time-averaged Nusselt Number under Different Inlet Steam Superheat Degrees
图 15 不同初始壁面温度下包壳平均热流密度变化趋势
Figure 15. Variation Trends of Average Heat Flux of Cladding under Different Initial Wall Surface Temperatures
图 16 不同初始壁面温度下蒸汽平均温度变化趋势
Figure 16. Variation Trends of Average Steam Temperature under Different Initial Wall Surface Temperatures
图 17 不同初始壁面温度下平均对流换热系数变化趋势
Figure 17. Variation Trends of Average Convective Heat Transfer Coefficient under Different Initial Wall Surface Temperatures
图 18 不同初始壁面温度下时均雷诺数、时均努塞尔数变化趋势
Figure 18. Variation Trends of Time-averaged Reynolds Number and Time-averaged Nusselt Number under Different Initial Wall Surface Temperatures
图 19 不同出口蒸汽压力下包壳平均热流密度变化趋势
Figure 19. Variation Trends of Average Cladding Heat Flux under Different Outlet Steam Pressures
图 20 不同出口蒸汽压力下包壳平均壁面温度变化趋势
Figure 20. Variation Trends of Average Cladding Wall Temperature of under Different Outlet Steam Pressures
图 21 不同出口蒸汽压力下蒸汽平均温度变化趋势
Figure 21. Variation Trends of Average Steam Temperature under Different Outlet Steam Pressures
图 22 不同出口蒸汽压力下平均对流换热系数变化趋势
Figure 22. Variation Trends of Average Convective Heat Transfer Coefficient under Different Outlet Steam Pressures
图 23 不同出口蒸汽压力下时均雷诺数、时均努塞尔数变化趋势
Figure 23. Variation Trends of Time-averaged Reynolds Number and Time-averaged Nusselt Number under Different Outlet Steam Pressures
图 24 不同栅径比下包壳平均热流密度变化趋势
Figure 24. Variation Trends of Average Cladding Heat Flux under Different Grid Diameter Ratios
图 25 不同栅径比下包壳平均壁面温度变化趋势
Figure 25. Variation Trends of Average Cladding Wall Temperature under Different Grid Diameter Ratios
图 26 不同栅径比下蒸汽平均温度变化趋势
Figure 26. Variation Trends of Average Steam Temperature under Different Grid Diameter Ratios
图 27 不同栅径比下平均对流换热系数变化趋势
Figure 27. Variation Trends of Average Convective Heat Transfer Coefficient under Different Grid Diameter Ratios
图 28 不同栅径比下时均雷诺数、时均努塞尔数变化趋势
Figure 28. Variation Trends of Time-averaged Reynolds Number and Time-averaged Nusselt Number under Different Grid Diameter Ratios
图 29 不同经验关联式与LES结果对比
Figure 29. Comparison of Different Empirical Correlations and LES Results
图 30 修正后的D-B关联式与LES结果对比
Figure 30. Comparison of the Corrected Dittus-Boelter Correlation with LES Results
表 1 棒束通道几何参数
Table 1. Geometric Parameters of the Rod Bundle Channel
参数名 参数值 包壳内、外径/mm 8.360、9.500 气隙内、外径/mm 8.138、8.360 UO2芯块直径/mm 8.138 燃料棒长度/mm 1000 栅径比 1.33/1.20/1.06 
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表 2 过热蒸汽物性参数[12]
Table 2. Physical Property Parameters of Superheated Steam
温度/K 密度/(kg·m−3) 定压比热/(J·kg−1·K−1) 热导率/(W·m−1·K−1) 运动粘度/(m2·s−1) 533.15 0.41312 1993.7 0.03936 4.33×10−5 633.15 0.34733 2045.8 0.05009 6.34×10−5 733.15 0.29974 2108.1 0.06173 8.72×10−5 833.15 0.26366 2175.2 0.07407 1.15×10−4 933.15 0.23536 2245.0 0.08698 1.45×10−4 1033.15 0.21255 2315.4 0.10035 1.79×10−4 1133.15 0.19378 2385.0 0.11409 2.17×10−4 1233.15 0.17805 2452.2 0.12812 2.57×10−4
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表 3 本研究相关边界条件
Table 3. Boundary Conditions Relevant to This Study
序号 栅径比 出口蒸汽压力/MPa 入口蒸汽过热度/K 入口蒸汽速度/(m·s−1) 初始壁面温度/K 衰变热/(W·m−1) Rein 工况1 1.33 0.10 100 10 923.15 2500 2950.99 工况2 1.33 0.10 150 10 923.15 2500 2365.71 工况3 1.33 0.10 150 15 923.15 2500 3548.57 工况4 1.33 0.10 150 20 923.15 2500 4731.42 工况5 1.33 0.10 150 25 923.15 2500 5914.28 工况6 1.33 0.10 150 30 923.15 2500 7097.14 工况7 1.33 0.10 200 10 923.15 2500 1937.90 工况8 1.33 0.10 150 10 773.15 2500 2365.71 工况9 1.33 0.10 150 10 1073.15 2500 2365.71 工况10 1.20 0.10 150 20 923.15 2500 3655.21 工况11 1.06 0.10 150 20 923.15 2500 2551.10 工况12 1.33 0.25 150 10 923.15 2500 5877.82 工况13 1.33 0.40 150 10 923.15 2500 9471.24
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