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利用格子玻尔兹曼方法(lattice Boltzmann method, LBM)对倾斜多孔介质方腔内Al2O3-H2O纳米流体的自然对流进行数值模拟, 考虑了孔隙率(0.3 ≤
$\epsilon $ ≤ 0.9)、瑞利数(103 ≤ Ra ≤ 106)、纳米颗粒体积分数(0 ≤ ϕ ≤ 0.04)和倾斜角(0° ≤ γ ≤ 120°)等因素的影响, 研究了正弦温度分布边界条件下倾斜多孔介质方腔内纳米流体的自然对流传热机理. 结果表明: 若$\epsilon $ 和γ保持不变时, 随着Ra数的增大, 热壁面处的平均努塞尔数(Nuave数)呈现出先减小后增大的趋势; 对于给定的Ra数, 当γ = 0°时, 随着孔隙率的增大, 热壁面处Nuave数逐渐增大, 当γ = 40°, 80°和120°时, Nuave数在$\epsilon $ = 0.7左右时达到最大值; 若$\epsilon $ 和Ra数保持不变, 当γ = 40°时, 方腔内的自然对流换热效率最强, 当γ = 80°时热壁面自然对流换热效率被削弱. 最后, 研究了纳米颗粒体积份数的影响, 当方腔施加一定倾角时, 热壁面处的Nuave数随着纳米颗粒体积分数的增大而增大.In this work, numerical simulation of nature convection of Al2O3-H2O nanofluid in an inclined square porous enclosure is investigated to analyze the influence of different physical parameters on fluid flow and heat transfer via the lattice Boltzmann method. Due to stable chemical properties and low price in the dispersion system, Al2O3-H2O nanofluid is widely used in the field of industrial heat transfer enhancement, which is the focus of present work. When the nanofluid is transport in a porous media, the Darcy-Brinkman-Forchheimer model is usually used to describe the porous media effects on nanofluid flow. Compared with uniform thermal boundary condition, the natural convection of nanofluids with non-uniform thermal boundary condition has not received much attention. In this paper, the sinusoidal boundary condition is applied to the left side wall to analyze the heat transfer mechanism of Al2O3-H2O nanofluid in the inclined square porous enclosure. The effect of porosity (0.3 ≤$\epsilon $ ≤ 0.9), Rayleigh number (103 ≤ Ra ≤ 106), volume fraction of nanoparticle (0 ≤ ϕ ≤ 0.04), tilt angle (0° ≤ γ ≤ 120°) on the heat transfer performance are systematically investigated. Numerical results show that the non-uniform boundary condition can affect the heat transfer performance on Al2O3-H2O nanofluid with different physical quantities, which is different from the uniform boundary condition. When γ = 0° and Ra is fixed, the Nuave number (average Nusselt number) at the heated wall increases with porosity. When γ = 40°, 80° or 120°, the Nuave reaches its maximum value at$\epsilon $ = 0.7. In addition, if$\epsilon $ and Ra are fixed, the results show that the heat transfer performance is most efficient at γ = 40° whereas it is weakened at γ = 80°. Moreover, when different inclination angles are applied to the square cavity, the Nuave increases slightly with an augmentation of ϕ. In all, compared with the uniform temperature boundary condition, the effect of volume fraction of nanoparticles on the enhanced heat transfer is not significant, therefore, to improve the heat transfer performance of nanofluids with given ϕ and Ra, it is necessary to take advantage of the improvement of effective thermal conductivity for the nanofluids in porous media and the perturbation influence of inclination angles on the system together with using appropriate porosity and square cavity tilt angle to intervene the flow.-
Keywords:
- nanofluids /
- nature convection /
- non-equilibrium temperature distribution /
- lattice Boltzmann method
[1] Kefayati G 2017 Int. J. Heat Mass Transfer 112 709
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[2] 李新芳, 朱冬生 2009 低温与超导 37 67
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Li X F, Zhu D S 2009 Cryogenics & Superconductivity 37 67
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Zhang J, Bai G J, Ma W Q, Wang G 2017 Journal of Gansu Sciences 29 110
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[21] Ashorynejad H R, Hoseinpour B 2017 J. Theor. Appl. Mech. 62 86
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[26] Selimefendigil F, Öztop H 2014 Int. J. Heat Mass Transfer 78 741
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[27] Seta T, Takegoshi E, Okui K 2006 Math. Comput. Simul. 72 195
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[28] Mohamad A, Kuzmin A 2010 Int. J. Heat Mass Transfer 53 990
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[29] Sajjadi H, Delouei A A, Atashafrooz M, Sheikholeslami M 2018 Int. J. Heat Mass Transfer 126 489
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图 2 不同
$ \epsilon $ 下温度场和流场的分布图像 (a)$\epsilon $ = 0.3; (b)$\epsilon $ = 0.5; (c)$\epsilon $ = 0.7; (d)$\epsilon $ = 0.9Fig. 2. Streamlines, isotherms contours for different
$\epsilon $ : (a)$\epsilon $ = 0.3; (b)$\epsilon $ = 0.5; (c)$\epsilon $ = 0.7; (d)$\epsilon $ = 0.9.
图 3 (a)不同
$ \epsilon $ 下X = 0处的竖直速度分布; (b) Y = 1处的水平速度分布图Fig. 3. (a) Vertical velocity distribution at X = 0; (b) horizontal velocity distribution at Y = 1 for different
$\epsilon $ .
图 4 (a)不同
$\epsilon $ 下热壁面处Nuave数分布曲线; (b)热壁面处局部Nu数分布曲线Fig. 4. (a) At the heated wall Nuave number; (b) local Nu number for different
$\epsilon $ .
图 5 不同Ra下温度场和流场的分布图像 (a) Ra = 103; (b) Ra = 104; (c) Ra = 105; (d) Ra = 106
Fig. 5. Streamlines, isotherms contours for different Ra number: (a) Ra = 103; (b) Ra = 104; (c) Ra = 105; (d) Ra = 106.
图 6 (a) 不同Ra下X = 0处的竖直速度分布; (b) Y = 1处的水平速度分布图
Fig. 6. (a) Vertical velocity distribution at X = 0; (b) horizontal velocity distribution at Y = 1 for different
$\epsilon $ .
图 7 (a)不同下Ra热壁面处Nuave数; (b)热壁面处局部Nu数分布曲线
Fig. 7. (a) At the heated wall Nuave number; (b) local Nu number for different Ra.
图 8 不同γ下温度场和流场的分布图像 (a) γ = 0°; (b) γ = 40°; (c) γ = 80°; (d) γ = 120°
Fig. 8. Streamlines, isotherms contours for different γ number: (a) γ = 0°; (b) γ = 40°; (c) γ = 80°; (d) γ = 120°.
图 9 (a)不同γ时Y = 0.5处局部温度分布曲线; (b)热壁面处Vave/Nuave的分布曲线
Fig. 9. (a) Local temperature distribution along the Y = 0.5; (b) average velocity in the y direction & Nuave number at the heated wall in different γ.
图 10 (a)不同γ下热壁面处局部竖直速度V; (b)热壁面处局部Nu数的分布曲线
Fig. 10. (a) Local velocity in the y direction; (b) local Nuave number at the heated wall in different γ.
图 11 (a)随着
$\epsilon $ 的增加不同γ时热壁面Nuave数分布曲线; (b)当γ = 0°, 40°时, 不同$\epsilon $ 下局部Nu数的分布曲线Fig. 11. (a) Variation of Nuave number as a function of
$\epsilon $ in different γ at the heated wall; (b) when γ = 0°, 40°, variation of local Nu number at the heated wall in different$\epsilon $ .
图 12 (a)随着ϕ的增加不同γ下热壁面Nuave数分布曲线; (b)当γ = 0°, 40°时, 不同ϕ下局部Nu数的分布曲线
Fig. 12. (a) Variation of Nuave number as a function of ϕ in different γ at the heated wall; (b) when γ = 0°, 40°, variation of local Nu number at the heated wall in different ϕ.
表 1 H2O, Al2O3和玻璃纤维的热物理性质
Table 1. Thermophysical properties of water, Al2O3 and glass fibers.
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表 2 纳米流体的热物性参数计算公式
Table 2. Calculation formula for thermodynamic properties of nanofluids.
热物性参数 计算表达式 纳米流体粘度 $\mu {}_{nf} = \dfrac{{{\mu _f}}}{{{{\left( {1 - \phi } \right)}^{2.5}}}}$ 纳米流体密度 ${\rho _{nf}} = \left( {1 - \phi } \right){\rho _f} + \phi {\rho _s}$ 纳米流体热容 ${\left( {\rho {C_p}} \right)_{nf}} = \left( {1 - \phi } \right){\left( {\rho {C_p}} \right)_f} + \phi {\left( {\rho {C_p}} \right)_s}$ 纳米流体热扩散系数 ${\alpha _{nf}} = \dfrac{{{k_{nf}}}}{{{{\left( {\rho {C_p}} \right)}_{nf}}}}$ 纳米流体热膨胀系数 ${\left( {\rho \beta } \right)_{nf}} = \left( {1 - \phi } \right){\left( {\rho \beta } \right)_f} + \phi {\left( {\rho \beta } \right)_s}$ 纳米流体导热系数 ${k_{nf}} = \dfrac{{{k_p} + 2{k_f} - 2\left( {{k_f} - {k_p}} \right)\phi }}{{{k_p} + 2{k_f} + 2\left( {{k_f} - {k_p}} \right)\phi }}{k_f}$ 多孔介质有效
导热系数${k_m} = \left( {1 - \epsilon} \right){k_p} + {\epsilon k_{nf}}$
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表 3 不同网格数与文献[33]的Nuave数比较
Table 3. Comparison of Nuave number with literature[33] in different grids number.
不同网格数下的Nuave数 80 × 80 100 × 100 120 × 120 140 × 140 Nuave数 8.528 8.670 8.744 8.785 误差/% 3.39% 1.70% 0.83% 0.36%
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[1] Kefayati G 2017 Int. J. Heat Mass Transfer 112 709
Google Scholar
[2] 李新芳, 朱冬生 2009 低温与超导 37 67
Google Scholar
Li X F, Zhu D S 2009 Cryogenics & Superconductivity 37 67
Google Scholar
[3] 张晶, 白国君, 马文强, 王刚 2017 甘肃科学学报 29 110
Zhang J, Bai G J, Ma W Q, Wang G 2017 Journal of Gansu Sciences 29 110
[4] Khanafer K, Vafai K, Lightstone M 2003 Int. J. Heat Mass Transfer 46 3639
Google Scholar
[5] Hatami M 2017 J. Mol. Liq. 233 1
Google Scholar
[6] Chen S, Du R 2011 Energy 36 1721
Google Scholar
[7] Selimefendigil F, Öztop H F 2016 J. Mol. Liq. 216 67
Google Scholar
[8] Hatami M 2017 Journal of Molecular Liquids 233 1
[9] Jahanshahi M, Hosseinizadeh S F, Alipanah M, Dehghani A, Vakilinejad G R 2010 Int. Commun. Heat Mass Transfer 37 687
Google Scholar
[10] Mackie C, Desai P, Meyers C 1999 Int. J. Heat Mass Transfer 42 3337
Google Scholar
[11] Khair K 1985 Int. J. Heat Mass Transfer 28 909
Google Scholar
[12] Lam P, Prakash K 2014 Int. J. Heat Mass Transfer 69 390
Google Scholar
[13] Kaluri R, Basak T 2011 Energy 36 5065
Google Scholar
[14] Alsabery A, Chamkha A, Saleh H, Hashim I 2017 Int. J. Heat Mass Transfer 7 2357
[15] Toosi M H, Siavashi M 2017 J. Mol. Liq. 238 553
Google Scholar
[16] Wu F, Zhou W, Ma X 2015 Int. J. Heat Mass Transfer 85 756
Google Scholar
[17] Basak T, Roy S, Paul T, Pop I 2006 Int. J. Heat Mass Transfer 49 1430
Google Scholar
[18] Ghasemi K, Siavashi M 2017 J. Mol. Liq. 233 415
Google Scholar
[19] Sivasankaran S, Alsabery A I, Hashim I 2018 Phys. A (Amsterdam, Neth.) 509 275
Google Scholar
[20] Ho C J, Chen M W, Li Z W 2008 Int. J. Heat Mass Transfer 51 4506
Google Scholar
[21] Ashorynejad H R, Hoseinpour B 2017 J. Theor. Appl. Mech. 62 86
[22] Nield D A, Bejan A 2006 Convection in Porous Media (Vol. 3) (New York: Springer) pp37–55
[23] Grott M, Knollenberg J, Krause C 2010 J. Geophys. Res.: Planets 115 E11005
Google Scholar
[24] Reddy K S, Sreedhar D 2016 Int. J. Curr. Eng. Technol. 6 2277
[25] Sheikholeslami M, Gorji-Bandpy M, Domiri Ganji D 2013 Energy 60 501
Google Scholar
[26] Selimefendigil F, Öztop H 2014 Int. J. Heat Mass Transfer 78 741
Google Scholar
[27] Seta T, Takegoshi E, Okui K 2006 Math. Comput. Simul. 72 195
Google Scholar
[28] Mohamad A, Kuzmin A 2010 Int. J. Heat Mass Transfer 53 990
Google Scholar
[29] Sajjadi H, Delouei A A, Atashafrooz M, Sheikholeslami M 2018 Int. J. Heat Mass Transfer 126 489
Google Scholar
[30] Sajjadi H, Kefayati G 2015 Heat Transf. Asian Res. 45 795
[31] Javadi K, Kazemi K 2018 Phys. Fluids 30 017104
Google Scholar
[32] Sadr M, Gorji H 2017 Phys. Fluids 29 122007
Google Scholar
[33] Davis G D V, Jones I P 1983 Int. J. Numer. Methods Fluids 3 227
Google Scholar
[34] Nithiarasu P, Seetharamu K N, Sundararajan T 1997 Int. J. Heat Mass Transfer 40 3955
Google Scholar
[35] Wang J, Lou Q, Xu H, Chen J, Yang M 2018 Int. Commun. Heat Mass Transf. 35 405
[36] Kefayati G H R 2018 Int. J. Heat Mass Transfer 116 762
Google Scholar
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