Effect of liquid viscosity on hydrodynamics and bubble behaviour of an external‐loop airlift reactor

Wu, Qian; Wang, Xuekui; Wang, Tiefeng; Han, Mei; Sha, Zuoliang; Wang, Jinfu

doi:10.1002/cjce.21788

Cited by 18 publications

(10 citation statements)

References 23 publications

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“…The present state of the art of correlations [22][23][24][25][26][27][28] predicting the gas holdup in air-water 1 glycerol systems at U G 5 0.05 m/s is summarized in Figure 2. Except for Sotelo et al, 25 a reduction of the gas holdup with increasing liquid viscosity was observed.…”

Section: Introductionmentioning

confidence: 99%

“…Except for Sotelo et al, 25 a reduction of the gas holdup with increasing liquid viscosity was observed. [22][23][24][25][26][27][28] Apart from the available correlations, there are some controversial reports on the effect of the liquid viscosity on the gas holdup. 19,[29][30][31][32] An increase of gas holdup was found at low liquid viscosity l 3-4 mPa-s, a decrease at moderate viscosity l 5 3-11 mPa-s and roughly constant gas holdup at a higher viscosity.…”

Section: Introductionmentioning

confidence: 99%

“…Much research has been devoted to the effect of liquid properties on the gas holdup [17][18][19][20][21][22][23][24][25][26][27][28] over the last decades. The present state of the art of correlations [22][23][24][25][26][27][28] predicting the gas holdup in air-water 1 glycerol systems at U G 5 0.05 m/s is summarized in Figure 2.…”

Section: Introductionmentioning

confidence: 99%

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Regime transition in viscous and pseudo viscous systems: A comparative study

2014

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A comprehensive quantitative study on the effect of liquid viscosity (1 l L 1149 mPa-s) on the local flow phenomena of the gas phase in a small diameter bubble column is performed using ultrafast electron beam X-ray tomography. The internal dynamic flow structure and the bubble size distribution shows a dual role of the liquid viscosity on the hydrodynamics. Further, the effect of solid concentration (C s 5 0.05, 0.20) on the local flow behavior of the gas phase is studied for the pseudo slurry viscosities similar to the liquid viscosities of the gas-liquid systems. The effects of liquid and pseudo slurry viscosities on flow structure, bubble size distribution, and gas phase distribution are compared. The bubble coalescence is significantly enhanced with the addition of particles as compared to the system without particles for apparently same viscosity. The superficial gas velocity at which transition from homogeneous bubbly to slug flow regime occurs is initiated by the addition of particles as compared to the particle free system for apparently same viscosity. V C

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Section: Introductionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Regime transition in viscous and pseudo viscous systems: A comparative study

2014

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“…The volume of gas bubble is influenced by the physical properties of system, especially the viscosity of slag phase. 21) Therefore, this difference would be caused by the high viscosity of slag. When the gas flow rate increased to 300 NmL/min and higher, the difference in the gas bubble volume between the two systems became more marked.…”

Section: Resultsmentioning

confidence: 99%

Metal Emulsion in Sn Alloy/oxide System by Bottom Gas Injection

et al. 2017

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A metal emulsion is formed by the passage of gas bubbles through the interface between the metal phase and the slag phase in the steelmaking process. Emulsified metal droplets have great potential to improve the chemical reaction efficiency during motion in bulk slag. Several studies have focused on the formation mechanism of metal droplets and on the influence of the physical properties of the system on this mechanism. In this study, Sn alloy and sodium tetraborate were used to simulate molten steel and slag, respectively. Gas bubbles were introduced from the bottom of a molten metal bath at various gas flow rates. Slag containing metal droplets at the center of the slag phase was sampled, and the metal droplets were extracted by the dissolution of the oxide in a solvent. The number and diameter of the droplets were measured using a digital microscope. Under the same experimental conditions, the number of metal droplets in the oxide system was smaller but their size was larger than those in a previously investigated Sn alloy/chloride system. In both the systems, the total mass of metal droplets formed by a single bubble increased with an increase in the volume of the gas bubble, and when the volume of the gas bubble was small, the total mass of droplets in the oxide system was smaller than that in the chloride system. The sedimentation rate and coefficient in the oxide system were lower than those in the chloride system.

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“…A single bubble rising in a quiescent (or stagnant) liquid pool has been characterized by a number of previous studies. For instance, Luther et al [15], Cieslinski and Mosdorf [16], Ohta et al [17], and Wu et al [18] investigated the behavior of single bubble in the airlift reactor. Bunner and Tryggvason [19], Lu and Tryggvason [20], and Ziegenhein and Lucas [21] observed the characters of bubbles in vertical bubbly flow.…”

Section: Introductionmentioning

confidence: 99%

Optimization and Extended Applicability of Simplified Slug Flow Model for Liquid-Gas Flow in Horizontal and Near Horizontal Pipes

et al. 2020

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The accurate prediction of pressure loss for two-phase slug flow in pipes with a simple and powerful methodology has been desired. The calculation of pressure loss has generally been performed by complicated mechanistic models, most of which require the iteration of many variables. The objective of this study is to optimize the previously proposed simplified slug flow model for horizontal pipes, extending the applicability to turbulent flow conditions, i.e., high mixture Reynolds number and near horizontal pipes. The velocity field previously measured by particle image velocimetry further supports the suggested slug flow model which neglects the pressure loss in the liquid film region. A suitable prediction of slug characteristics such as slug liquid holdup and translational velocity (or flow coefficient) is required to advance the accuracy of calculated pressure loss. Therefore, the proper correlations of slug liquid holdup, flow coefficient, and friction factor are identified and utilized to calculate the pressure gradient for horizontal and near horizontal pipes. The optimized model presents a fair agreement with 2191 existing experimental data (0.001 ≤ μL ≤ 0.995 Pa∙s, 7 ≤ ReM ≤ 227,007 and −9 ≤ θ ≤ 9), showing −3% and 0.991 as values of the average relative error and the coefficient of determination, respectively.

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Effect of liquid viscosity on hydrodynamics and bubble behaviour of an external‐loop airlift reactor

Cited by 18 publications

References 23 publications

Regime transition in viscous and pseudo viscous systems: A comparative study

Regime transition in viscous and pseudo viscous systems: A comparative study

Metal Emulsion in Sn Alloy/oxide System by Bottom Gas Injection

Optimization and Extended Applicability of Simplified Slug Flow Model for Liquid-Gas Flow in Horizontal and Near Horizontal Pipes

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