Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process

doi:10.1016/j.cjche.2023.09.003

中国化学工程学报 ›› 2024, Vol. 65 ›› Issue (1): 243-254.DOI: 10.1016/j.cjche.2023.09.003

• Full Length Article • 上一篇下一篇

Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process

Xiemin Liu¹, Jing Wan¹, Jinnan Sun¹, Lin Zhang², Feng Zhang¹, Zhibing Zhang¹, Xinyao Li¹, Zheng Zhou¹

1 Key Laboratory of Mesoscopic Chemistry of Ministry of Education (MOE), School of Chemistry and Chemical Engineering, Nanjing University, Nanjing 210023, China;
2 Dalian Research Institute of Petroleum and Petrochemicals, SINOPEC, Dalian 116045, China

收稿日期:2023-07-07 修回日期:2023-09-21 出版日期:2024-01-28 发布日期:2024-04-17
通讯作者: Feng Zhang,E-mai:zf@nju.edu.cn;Zhibing Zhang,E-mai:zbzhang@nju.edu.cn
基金资助:
The authors are grateful for the financial support of the National Natural Science Foundation of China (21776122).

Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process

Xiemin Liu¹, Jing Wan¹, Jinnan Sun¹, Lin Zhang², Feng Zhang¹, Zhibing Zhang¹, Xinyao Li¹, Zheng Zhou¹

1 Key Laboratory of Mesoscopic Chemistry of Ministry of Education (MOE), School of Chemistry and Chemical Engineering, Nanjing University, Nanjing 210023, China;
2 Dalian Research Institute of Petroleum and Petrochemicals, SINOPEC, Dalian 116045, China

Received:2023-07-07 Revised:2023-09-21 Online:2024-01-28 Published:2024-04-17
Contact: Feng Zhang,E-mai:zf@nju.edu.cn;Zhibing Zhang,E-mai:zbzhang@nju.edu.cn
Supported by:
The authors are grateful for the financial support of the National Natural Science Foundation of China (21776122).

摘要/Abstract

摘要： Due to a prolonged operation time and low mass transfer efficiency, the primary challenge in the aeration process of non-Newtonian fluids is the high energy consumption, which is closely related to the form and rate of impeller, ventilation, rheological properties and bubble morphology in the reactor. In this perspective, through optimal computational fluid dynamics models and experiments, the relationship between power consumption, volumetric mass transfer rate (k_La) and initial bubble size (d₀) was constructed to establish an efficient operation mode for the aeration process of non-Newtonian fluids. It was found that reducing the d₀ could significantly increase the oxygen mass transfer rate, resulting in an obvious decrease in the ventilation volume and impeller speed. When d₀ was regulated within 2-5 mm, an optimal k_La could be achieved, and 21% of power consumption could be saved, compared to the case of bubbles with a diameter of 10 mm.

关键词: Non-Newtonian fluids aeration process, Power consumption, Volumetric mass transfer rate, Bubble size

Abstract: Due to a prolonged operation time and low mass transfer efficiency, the primary challenge in the aeration process of non-Newtonian fluids is the high energy consumption, which is closely related to the form and rate of impeller, ventilation, rheological properties and bubble morphology in the reactor. In this perspective, through optimal computational fluid dynamics models and experiments, the relationship between power consumption, volumetric mass transfer rate (k_La) and initial bubble size (d₀) was constructed to establish an efficient operation mode for the aeration process of non-Newtonian fluids. It was found that reducing the d₀ could significantly increase the oxygen mass transfer rate, resulting in an obvious decrease in the ventilation volume and impeller speed. When d₀ was regulated within 2-5 mm, an optimal k_La could be achieved, and 21% of power consumption could be saved, compared to the case of bubbles with a diameter of 10 mm.

Key words: Non-Newtonian fluids aeration process, Power consumption, Volumetric mass transfer rate, Bubble size

Xiemin Liu, Jing Wan, Jinnan Sun, Lin Zhang, Feng Zhang, Zhibing Zhang, Xinyao Li, Zheng Zhou. Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process[J]. 中国化学工程学报, 2024, 65(1): 243-254.

参考文献

[1] R. Chhabra, J.F. Richardson, Non-Newtonian Flow and Applied Rheology:Engineering Applications, Butterworth-Heinemann, Oxford, 2011.
[2] J.C. Gabelle, E. Jourdier, R.B. Licht,F. Ben Chaabane, I. Henaut, J. Morchain, F. Augier, Impact of rheology on the mass transfer coefficient during the growth phase of Trichoderma reesei in stirred bioreactors, Chem. Eng. Sci. 75(2012)408-417.
[3] F. Garcia-Ochoa, E. Gomez, A. Alcon, V.E. Santos, The effect of hydrodynamic stress on the growth of Xanthomonas campestris cultures in a stirred and sparged tank bioreactor, Bioprocess Biosyst. Eng. 36(7)(2013)911-925.
[4] D. Malik, L. Pakzad, Experimental investigation on an aerated mixing vessel through electrical resistance tomography (ERT) and response surface methodology (RSM), Chem. Eng. Res. Des. 129(2018)327-343.
[5] V. Cappello, C. Plais, C. Vial, F. Augier, Scale-up of aerated bioreactors:CFD validation and application to the enzyme production by Trichoderma reesei, Chem. Eng. Sci. 229(2021)116033.
[6] F. Liu, A. Ouedraogo, S. Manghee, A. Danilenko, A Primer on Energy Efficiency for Municipal Water and Wastewater Utilities, Energy Sector Management Assistance Program © World Bank, Washington, DC, 2012. Technical Report 001/12.
[7] D. Mamais, C. Noutsopoulos, A. Dimopoulou, A. Stasinakis, T.D. Lekkas, Wastewater treatment process impact on energy savings and greenhouse gas emissions, Water Sci. Technol. 71(2)(2015)303-308.
[8] G.Q. Li, H.W. Qiu, Z.M. Zheng, Z.L. Cai, S.Z. Yang, Effect of fluid rheological properties on mass transfer in a bioreactor, J. Chem. Technol. Biotechnol. 62(4)(1995)385-391.
[9] F. García-Ochoa, E. Gomez, Mass transfer coef ficient in stirred tank reactors for xanthan gum solutions, Biochem. Eng. J. 1(1)(1998)1-10.
[10] B.Q. Liu, Q. Xiao, N. Sun, P.F. Gao, F.Y. Fan, B. Sunden, Effect of gas distributor on gaseliquid dispersion and mass transfer characteristics in stirred tank, Chem. Eng. Res. Des. 145(2019)314-322.
[11] S.S. Alves, C.I. Maia, J.M.T. Vasconcelos, A.J. Serralheiro, Bubble size in aerated stirred tanks, Chem. Eng. J. 89(1-3)(2002)109-117.
[12] S. Jegatheeswaran, A. Kazemzadeh, F. Ein-Mozaffari, Enhanced aeration efficiency in non-Newtonian fluids using coaxial mixers:High-solidity ratio central impeller with an anchor, Chem. Eng. J. 378(2019)122081.
[13] S.J. Arjunwadkar, K. Sarvanan, P.R. Kulkarni, A.B. Pandit, Gaseliquid mass transfer in dual impeller bioreactor, Biochem. Eng. J. 1(2)(1998)99-106.
[14] S.J. Arjunwadkar, K. Saravanan, A.B. Pandit, P.R. Kulkarni, Optimizing the impeller combination for maximum hold-up with minimum power consumption, Biochem. Eng. J. 1(1)(1998)25-30.
[15] J.C. Gabelle, F. Augier, A. Carvalho, R. Rousset, J. Morchain, Effect of tank size on k_La and mixing time in aerated stirred reactors with non-Newtonian fluids, Can. J. Chem. Eng. 89(5)(2011)1139-1153.
[16] V. Cappello, C. Plais, C. Vial, F. Augier, Bubble size and liquid-side mass transfer coefficient measurements in aerated stirred tank reactors with nonNewtonian liquids, Chem. Eng. Sci. 211(2020)115280.
[17] F. García-Ochoa, E.G. Castro, V.E. Santos, Oxygen transfer and uptake rates during xanthan gum production, Enzyme Microb. Technol. 27(9)(2000)680-690.
[18] M. Jamshidzadeh, F. Ein-Mozaffari, A. Lohi, Experimental analysis of the mass transfer coefficient and interfacial area in an aerated coaxial mixing system comprising a non-Newtonian solution, Ind. Eng. Chem. Res. 59(49)(2020)21530-21547.
[19] A. Tomiyama, Struggle with computational bubble dynamics, Multiph. Sci. Technol. 10(4)(1998)369-405.
[20] M. Bla zej, J. Annus, J. Marko s, Comparison of gassing-out and pressure-step dynamic methods for k_La measurement in an airlift reactor with internal loop, Chem. Eng. Res. Des. 82(10)(2004)1375-1382.
[21] I.J. Dunn, Airlift bioreactors, Chem. Eng. Sci. 44(12)(1989)3006.
[22] S. Zhang, Z.Y. Lv, D. Müller, G. Wozny, PBM-CFD investigation of the gas holdup and mass transfer in a lab-scale internal loop airlift reactor, IEEE Access 5(2017)2711-2719.
[23] M.J. Prince, H.W. Blanch, Bubble coalescence and break-up in air-sparged bubble columns, AIChE J. 36(10)(1990)1485-1499.
[24] H.A. Luo, Coalescence, Breakup and Liquid Circulation in Bubble Column Reactors, Dr. Ing, thesis, Department of Chemical Engineering, the Norwegian Institute of Technology, Trondheim, Norway, 1993.
[25] N. Yang, Q. Xiao, A mesoscale approach for population balance modeling of bubble size distribution in bubble column reactors, Chem. Eng. Sci. 170(2017)241-250.
[26] H.A. Luo, H.F. Svendsen, Theoretical model for drop and bubble breakup in turbulent dispersions, AIChE J. 42(5)(1996)1225-1233.
[27] L.C. Han, H.A. Luo, Y.J. Liu, A theoretical model for droplet breakup in turbulent dispersions, Chem. Eng. Sci. 66(4)(2011)766-776.
[28] L.C. Han, S.G. Gong, Y.Q. Li, N.N. Gao, J. Fu, H.A. Luo, Z.F. Liu, Influence of energy spectrum distribution on drop breakage in turbulent flows, Chem. Eng. Sci. 117(2014)55-70.
[29] F. Sporleder, Z. Borka, J. Solsvik, H.A. Jakobsen, On the population balance equation, Rev. Chem. Eng. 28(2-3)(2012)149-169.
[30] J. Solsvik, S. Tangen, H.A. Jakobsen, On the constitutive equations for fluid particle breakage, Rev. Chem. Eng. 29(5)(2013)241-356.
[31] W.B. Shi, X.G. Yang, M. Sommerfeld, J. Yang, X.Y. Cai, G. Li, Y. Zong, Modelling of mass transfer for gaseliquid two-phase flow in bubble column reactor with a bubble breakage model considering bubble-induced turbulence, Chem. Eng. J. 371(2019)470-485.
[32] V. Momiroski, S. Bhattacharya, M. Davoody, A.A. Bin Abdul Raman, R. Parthasarathy, Size distribution of bubbles in agitated viscous Newtonian and non-Newtonian solutions, Asia Pac. J. Chem. Eng. 13(6)(2018) -2267.
[33] Y.L. Wei, J.B. Qiu, H.R. Karimi, M. Wang, Model approximation for twodimensional Markovian jump systems with state-delays and imperfect mode information, Multidimens. Syst. Signal Process. 26(3)(2015)575-597.
[34] H.Z. Tian, S.F. Pi, Y.C. Feng, Z. Zhou, F. Zhang, Z.B. Zhang, One-dimensional drift-flux model of gas holdup in fine-bubble jet reactor, Chem. Eng. J. 386(2020)121222.
[35] B.R. Wang, G.Q. Yang, H.Z. Tian, X.B. Li, G.D. Yang, Y.K. Shi, Z. Zhou, F. Zhang, Z. B. Zhang, A new model of bubble Sauter mean diameter in fine bubbledominated columns, Chem. Eng. J. 393(2020)124673.
[36] N. Dukhan, Ö. Bağcı, M. Özdemir, Metal foam hydrodynamics:Flow regimes from pre-Darcy to turbulent, Int. J. Heat Mass Transf. 77(2014)114-123.
[37] T.P. de Carvalho, H.P. Morvan, D.M. Hargreaves, H. Oun, A. Kennedy, Porescale numerical investigation of pressure drop behaviour across open-cell metal foams, Transp. Porous Medium 117(2)(2017)311-336.
[38] G.R. Bouton, W.L. Luyben, Optimum economic design and control of a gas permeation membrane coupled with the hydrodealkylation (HDA) process, Ind. Eng. Chem. Res. 47(4)(2008)1221-1237.
[39] E. Peral, M. Martín, Optimal production of dimethyl ether from switchgrassbased syngas via direct synthesis, Ind. Eng. Chem. Res. 54(30)(2015)7465-7475.

Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process

Effect of bubble morphology and behavior on power consumption in non-Newtonian fluids’ aeration process

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