Numerical investigation on heat transfer characteristics of staggered tube bundles in cross flow
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摘要:
为验证基于大管径实验数据的经典传热关联式在小尺度管束传热问题上的适用性，针对横掠叉排管束的管外流动换热特性进行了数值研究。在建立了确定变几何结构合理网格密度的方法基础上，探究了大参数范围内管径、管间距比和雷诺数对管外传热努塞尔数和流动特征的影响规律。结果表明：①管排流动马赫数小于0.1时，雷诺数不变，管径对管外努塞尔数影响很小，不同管径对应的管外流动特征差别很小；②管间距比通过改变管外的流动特征来影响管外努塞尔数，且雷诺数和管径不变时，努塞尔数分布在特定管间距比范围内存在峰值区；③需要更为具体的分段函数来拟合传热关联式以准确预测努塞尔数。
Abstract:In order to verify the applicability of the classical heat transfer correlations mostly based on the experimental data of large tube diameter on heat transfer of small-scale tube bundle, the flow and heat transfer characteristics outside the staggered tube bundle in cross flow were numerically investigated. With a new method to determine the reasonable mesh density of variable geometry, the effects of tube diameter, tube pitch ratio and Reynolds number on Nusselt number and flow characteristics outside the tube bundle were studied within a large parameter range. The following conclusions can be obtained: （1） when flow Mach number was smaller than 0.1 and Reynolds number kept constant, the tube diameter had little effect on the Nusselt number because the flow characteristics outside the tube varied slightly with tube diameter; （2） the tube pitch ratio affected Nusselt number by changing the flow characteristics outside the tube, and there was a peak area of Nusselt number within a specific range of tube pitch ratio when the Reynolds number and tube diameter kept constant; （3） a more specific piecewise function was needed to fit the heat transfer correlation to accurately predict the Nusselt number.
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Key words:
- staggered tube bundle /
- Nusselt number /
- small-scale /
- tube diameter /
- pitch ratio /
- flow structure
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图 3 Nu随网格单元尺寸的变化（σ1-σ2-D=2.1-2.1-16.4 mm）
Figure 3. Variation of Nu with mesh element size （σ1-σ2-D =2.1-2.1-16.4 mm）
图 4 不同管排结构下Nu随网格单元尺寸的变化
Figure 4. Variation of Nu with mesh element size with different tube bundle structures
图 5 数值结果与茹氏实验数据的比较
Figure 5. Comparison between the numerical results and Zukauskas’ experimental data
图 7 管束附近的无量纲流场（Re=5000, σ1-σ2=2.1-2.1）
Figure 7. Dimensionless velocity field around the tube bundle （Re=5000, σ1-σ2=2.1-2.1）
图 8 管束附近的无量纲流场（Re=5000, σ1-σ2=1.25-1.25）
Figure 8. Dimensionless velocity field around the tube bundle （Re=5000, σ1-σ2=1.25-1.25）
图 10 管束沿程马赫数分布（Re=7000, σ1-σ2=2.1-2.1）
Figure 10. Mach number distribution along the tube bundle （Re=7000, σ1-σ2=2.1-2.1）
图 11 管束沿程静温分布（Re=7000, σ1-σ2=2.1-2.1）
Figure 11. Static temperature distribution along the tube bundle （Re=7000, σ1-σ2=2.1-2.1）
图 14 Nu随管间距比的变化（茹氏公式）
Figure 14. Variation of Nu with tube pitch ratios （Zukauskas correlation）
图 15 典型管间距比下的无量纲速度场（Re=7000）
Figure 15. Variation of dimensionless velocity field with some typical tube pitch ratios （Re=7000）
图 16 典型管间距比下的无量纲湍流强度场（Re=7000）
Figure 16. Variation of dimensionless turbulent intensity field with some tube pitch ratios （Re=7000）
图 17 管束周向无量纲速度型随管间距比的变化（Re=5000）
Figure 17. Variation of tube bundle circumferential dimensionless velocity profile with tube pitch ratios （Re=5000）
表 1 模型参数
Table 1. Model parameters
参数 数值 管径D/mm 0.5～16.4 横向管间距比${\sigma _1}$ 1.1～4.2 纵向管间距比${\sigma _2}$ 1.1～4.2 雷诺数$Re$ 1000～7000 
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表 2 确定的另外两种结构的网格尺寸
Table 2. Mesh element sizes for two other structures
σ1-σ2-D/mm 网格单元尺寸/mm 2.1-2.1-5 0.105 1.25-1.25-5 0.0625
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表 3 数值结果与茹氏实验数据的偏差
Table 3. Discrepancy between the numerical results and Zukauskas’ experimental data
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表 4 不同管径的对数换热温差
Table 4. Log-mean temperature difference at various tube diameters
D/mm 进口静温/K 出口静温/K 对数温差/K 0.5 287.18 310.42 43.32 1 287.45 313.78 41.14 3 288.00 313.68 40.98
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