One-dimensional interfacial area transport of vertical upward bubbly flow in narrow rectangular channel

Shen, Xiuzhong; Hibiki, Takashi; Ono, Takafumi; Sato, K.; Mishima, Kaichiro

doi:10.1016/j.ijheatfluidflow.2012.04.007

Cited by 38 publications

(7 citation statements)

References 20 publications

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“…6(a), their whole structures cannot be seen clearly in Fig 5 because their views are partly obstructed by swarms of small bubbles existing in the liquid film region between the large cap bubble and the pipe wall. The view obstruction feature in observing large cap bubbles in large diameter pipe is quite different from that in other flow channels (Dukler and Taitel, 1977;Shen et al, 2012b). This study partly observed the large cap bubbles and detected their behavior, their horizontal and vertical sizes and their shapes by observing their visible parts and the motions of small bubbles near pipe wall in the motion video.…”

Section: Flow Regimes and Their Transitionsmentioning

confidence: 81%

Bubbly-to-cap bubbly flow transition in a long-26m vertical large diameter pipe at low liquid flow rate

Shen

Hibiki

Nakamura

2015

International Journal of Heat and Fluid Flow

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Section: Flow Regimes and Their Transitionsmentioning

confidence: 81%

Bubbly-to-cap bubbly flow transition in a long-26m vertical large diameter pipe at low liquid flow rate

Shen

Hibiki

Nakamura

2015

International Journal of Heat and Fluid Flow

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“…In the present work, the approach changes the bubble number density n due to breakage and coalescence mechanisms. Shen et al (2012) measured the axial distributions of the interfacial area concentration under vertical bubble flow, and obtained the adjustable parameters in the simplified one-dimensional transport equation. Taghavi et al (2011) developed an approach to predict the gas diameter in a turbine stirred tank based on the previous study.…”

Section: Size Distribution For Bubblesmentioning

confidence: 99%

“…Shen et al (2012) measured the interfacial area transport by a four-sensor conductivity probe, and then obtained the experimental data to correlate previous parameters. In the present study, C RC , C, C WE and C TI are set to 0.004, 3, 0.002 and 0.085, respectively.…”

Section: Size Distribution For Bubblesmentioning

confidence: 99%

Simulation of the Bubble Behaviors for Gas–Liquid Dispersion in Agitated Vessel

Liu

Sheng

Han

et al. 2017

J. Chem. Eng. Japan / JCEJ

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The present study mainly investigates bubble behaviors in an agitated vessel. Computational uid dynamics provides a method for exploring the complex uid ow in an agitated vessel. A stirred tank model with transport equation for the interfacial area concentration and force equilibrium equation for bubbles under multi-forces is created for a 43-dm 3 agitated vessel. The model considers the breakage and coalescence mechanism of the bubbles. The local gas holdup is measured by ber-optical probe. After this, the bubble size distributions are calculated by the interfacial area concentration model. The simulations with validated models show good agreement with the experiments. From the simulation results, the area in which the gas holdup value is greater than 0.01 extends 37% in the upper circulation region when the rotation speed is increased to 40 rad/s from 20 rad/s. However, in the lower circulation, the gas holdup maintains a low level due to the existence of a "death zone". The simulations indicate that the bubble breakage mainly occurs in the impeller out ow region and the coalescence occurs in the upper circulation region. For bubble behaviors being in the lower circulation region, bubble coalescence or breakage is determined by the ow eld pattern in the vessel. Moreover, it is di cult for the simulation process to converge when the virtual mass force is considered and there is a lack of effective technology to measure it, which has led researchers to generally ignore this force. In order to analyze the virtual mass force, the present study utilizes computer programming which is based on the virtual mass force formula to obtain the force. The results show that at positions close to the impeller tip and the center of the upper region, the virtual mass force value is 0.015 and 0.017, respectively, but the value is approximately zero in the bulk of the tank. Hence, the bubble has two signi cant stages of acceleration process in the vessel.

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“…Shen et al [13] also carried out experiments involving vertical rectangular channels during the upward flow of two-phase water and air with the purpose of determining the volume ratios and flow velocities of the individual phases. Shen et al [14] also investigated losses generated by two-phase air-water flow during upward two-phase flow in vertical rectangular channels under pressure. The value of the interfacial surface is also affected by the thickness of the liquid film flow.…”

Section: Introductionmentioning

confidence: 99%

Hydrodynamics of Two-Phase Gas-Very Viscous Liquid Flow in Heat Exchange Conditions

Czernek

Witczak

2020

Energies

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This paper presents the results of analyses of the impact of heat transfer conditions on the hydrodynamics of downward co-current annular flow in vertical tubes of very viscous liquid and gas. The research was conducted within the range of gas velocities of 0–30.0 m/s and liquid velocities of 0.001–0.254 m/s, while the viscosity was in the unprecedented range of 0.046–3.5 Pas. The research demonstrates that the volume and nature of the liquid waves with various amplitudes and frequencies arising on the surface of the film are relative to the flow rate and viscosity of the gas phase. At the same time, we found that, under the condition of liquid cooling, an increase in viscosity resulted in the formation of a smooth interface whereas, under the conditions where the liquid is heated at the end of the channel section, a greater number of capillary waves were formed. This research resulted in the development of new dependencies which take into account the influence of selected thermal and flow parameters (including mass fraction) on the values of volumes specific to very viscous liquid film flows. These dependencies improve the accuracy of calculation by 8–10% and are fully applicable to the description of the performance of an apparatus with a hydraulically generated liquid film.

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One-dimensional interfacial area transport of vertical upward bubbly flow in narrow rectangular channel

Cited by 38 publications

References 20 publications

Bubbly-to-cap bubbly flow transition in a long-26m vertical large diameter pipe at low liquid flow rate

Bubbly-to-cap bubbly flow transition in a long-26m vertical large diameter pipe at low liquid flow rate

Simulation of the Bubble Behaviors for Gas–Liquid Dispersion in Agitated Vessel

Hydrodynamics of Two-Phase Gas-Very Viscous Liquid Flow in Heat Exchange Conditions

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