Momentum and heat transfer in two-phase bubble flow—II. A comparison between experimental data and theoretical calculations

Sato, Yoshifusa; Sadatomi, Michio; Sekoguchi, Kotohiko

doi:10.1016/0301-9322(81)90004-5

Cited by 62 publications

(19 citation statements)

References 5 publications

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“…Two contributions to the turbulent diffusivity of the liquid phase have been identified for bubble flow in channels: one contribution regards the inherent wall turbulence and does not depend on bubble agitation of the culture; the other contribution regards the turbulence caused by the bubbles. For columns operated batchwise with respect to the liquid phase—absence of net liquid flow—the bubble‐induced turbulence is dominant and the turbulent diffusivity depends on the gas flow rate according to the relationship:

{normalD}_{T} = 1.2 ε_{normalG} \frac{{normald}_{B}}{2} {normalU}_{B}

where ε G is the gas‐holdup, d B the Sauter mean bubble diameter, and U B the mean bubble slip velocity . Under operating conditions typical of a bubble‐column, ε G ranges between 2 and 10%, d B ranges between 2 and 10 mm, U B ranges between 10 and 30 cm/s.…”

Section: Resultsmentioning

confidence: 99%

“…Uniform gas-sparging at the bottom of the photobioreactor provides a sufficient culture mixing. Two contributions to the turbulent diffusivity of the liquid phase have been identified for bubble flow in channels: 58,64,65 one contribution regards the inherent wall turbulence and does not depend on bubble agitation of the culture; the other contribution regards the turbulence caused by the bubbles. For columns operated batchwise with respect to the liquid phase-absence of net liquid flow-the bubble-induced turbulence is dominant and the turbulent diffusivity depends on the gas flow rate according to the relationship:…”

Section: Flat Photobioreactorsmentioning

confidence: 99%

“…where e G is the gas-holdup, d B the Sauter mean bubble diameter, and U B the mean bubble slip velocity. 64,65 Under operating conditions typical of a bubble-column, e G ranges between 2 and 10%, d B ranges between 2 and 10 mm, U B ranges between 10 and 30 cm/s. According to Eq.…”

Section: Flat Photobioreactorsmentioning

confidence: 99%

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Photobioreactors for microalgal cultures: A Lagrangian model coupling hydrodynamics and kinetics

Olivieri

Gargiulo

Lettieri

et al. 2015

Biotechnol Progress

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Closed photobioreactors have to be optimized in terms of light utilization and overall photosynthesis rate. A simple model coupling the hydrodynamics and the photosynthesis kinetics has been proposed to analyze the photosynthesis dynamics due to the continuous shuttle of microalgae between dark and lighted zones of the photobioreactor. Microalgal motion has been described according to a stochastic Lagrangian approach adopting the turbulence model suitable for the photobioreactor configuration (single vs. two-phase flows). Effects of light path, biomass concentration, turbulence level and irradiance have been reported in terms of overall photosynthesis rate. Different irradiation strategies (internal, lateral and rounding) and several photobioreactor configurations (flat, tubular, bubble column, airlift) have been investigated. Photobioreactor configurations and the operating conditions to maximize the photosynthesis rate have been pointed out. Results confirmed and explained the common experimental observation that high concentrated cultures are not photoinhibited at high irradiance level.

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{normalD}_{T} = 1.2 ε_{normalG} \frac{{normald}_{B}}{2} {normalU}_{B}

Section: Resultsmentioning

confidence: 99%

Section: Flat Photobioreactorsmentioning

confidence: 99%

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Photobioreactors for microalgal cultures: A Lagrangian model coupling hydrodynamics and kinetics

Olivieri

Gargiulo

Lettieri

et al. 2015

Biotechnol Progress

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“…While the focus of applicationoriented studies is to formulate empirical correlations a) Electronic mail: s.g.huisman@utwente.nl for the net heat and mass transfer coefficients, fundamental research focuses on measuring and characterising the local flow statistics which leads to physical insight behind the observed correlations. In particular, recent studies in turbulent bubbly flows have investigated a variety of aspects such as: (i) bubble size and velocity distributions 11,12 , (ii) global heat and mass transport measurements [12][13][14] , (iii) computational studies with ideal boundary conditions 15,16 , (iv) liquid velocity and temperature profile 11,17,18 , (v) homogeneous and inhomogeneous bubble injection [17][18][19] , and (vi) natural and forced convection 16,[19][20][21][22][23] .…”

Section: Introductionmentioning

confidence: 99%

Twente mass and heat transfer water tunnel: Temperature controlled turbulent multiphase channel flow with heat and mass transfer

Gvozdic

Dung

Gils

et al. 2019

Review of Scientific Instruments

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A new vertical water tunnel with global temperature control and the possibility for bubble and local heat & mass injection has been designed and constructed. The new facility offers the possibility to accurately study heat and mass transfer in turbulent multiphase flow (gas volume fraction up to 8%) with a Reynolds-number range from 1.5 × 10 4 to 3 × 10 5 in the case of water at room temperature. The tunnel is made of highgrade stainless steel permitting the use of salt solutions in excess of 15% mass fraction. The tunnel has a volume of 300 L. The tunnel has three interchangeable measurement sections of 1 m height but with different cross sections (0.3 × 0.04 m 2 , 0.3 × 0.06 m 2 , 0.3 × 0.08 m 2 ). The glass vertical measurement sections allow for optical access to the flow, enabling techniques such as laser Doppler anemometry, particle image velocimetry, particle tracking velocimetry, and laser-induced fluorescent imaging. Local sensors can be introduced from the top and can be traversed using a built-in traverse system, allowing for e.g. local temperature, hot-wire, or local phase measurements. Combined with simultaneous velocity measurements, the local heat flux in single phase and two phase turbulent flows can thus be studied quantitatvely and precisely. arXiv:1902.05871v1 [physics.flu-dyn]

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“…(3) The turbulence intensity increases with the increase in void fraction, flow direction and radial direction. The predicted liquid velocities by using existing algebraic turbulence models of Sato et al [1,2] and Kataoka and Serizawa [3] were compared with the present experimental data. The comparison indicates that those models do not reasonably predict the liquid velocity distribution in a two-phase flow in a large diameter pipe mainly due to the defect in the predictive model of the liquid shear stress.…”

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confidence: 99%

Untitled

Shen¹,

Mishima²,

Nakamura³

2010

JAPANESE JOURNAL OF MULTIPHASE FLOW

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In this study, local measurements of flow parameters, such as void fraction, liquid velocity and turbulence intensity were performed in a vertical upward air-water two-phase flow in a 200 mm inner diameter and 24 m in height pipe by using a hot-film anemometer. The measured mean void fraction and mean liquid velocity agreed well with those by the differential pressure method and the liquid Venturi flow meter respectively. The experimental results are summarized as follows: (1) The radial profile of void fraction changes from a wall peak shape to a core peak shape and the radial profile of liquid velocity changes from a flat shape to a core peak shape as the flow develops. (2) When the average void fraction increases, the shape of void fraction radial profile changes from a wall peak to a core peak and the radial profile of liquid velocity shows a gradually increasing core peak shape. (3) The turbulence intensity increases with the increase in void fraction, flow direction and radial direction. The predicted liquid velocities by using existing algebraic turbulence models of Sato et al. [1,2] and Kataoka and Serizawa [3] were compared with the present experimental data. The comparison indicates that those models do not reasonably predict the liquid velocity distribution in a two-phase flow in a large diameter pipe mainly due to the defect in the predictive model of the liquid shear stress. It is necessary for us to establish a new model for the radial pressure distribution when we predict the liquid velocity distribution by using the measured void fraction distribution and algebraic turbulence models in a large diameter pipe.

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Momentum and heat transfer in two-phase bubble flow—II. A comparison between experimental data and theoretical calculations

Cited by 62 publications

References 5 publications

Photobioreactors for microalgal cultures: A Lagrangian model coupling hydrodynamics and kinetics

Photobioreactors for microalgal cultures: A Lagrangian model coupling hydrodynamics and kinetics

Twente mass and heat transfer water tunnel: Temperature controlled turbulent multiphase channel flow with heat and mass transfer

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