Falling-Film Evaporation on Tube Bundle with Plain and Enhanced Tubes—Part I: Experimental Results

Habert, Mathieu; Thome, John R.

doi:10.1080/08916152.2010.502045

Cited by 56 publications

(8 citation statements)

References 13 publications

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“…Their results showed that the heat transfer coefficient of falling film evaporation outside horizontal tubes increases by the increase in the liquid feeding, evaporation boiling temperature, and heat flux. Habert and Thome [9,10] performed falling film evaporation measurements on a single tube row bundle and a three-row tube bundle to obtain local heat transfer coefficients. They observed that in a single-row configuration, the heat transfer coefficient is mostly constant for a given heat flux in the plateau region until the onset of dryout is reached, followed by increasing dryout of the surface with a rapid decrease of the heat transfer toward the vapor phase heat transfer value at complete dryout.…”

Section: Introductionmentioning

confidence: 99%

Two-phase flow numerical simulation and experimental verification of falling film evaporation on a horizontal tube bundle

Bigham

Kouhikamali

Abadi

2014

Desalination and Water Treatment

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In this study, a two-phase flow investigation on falling film evaporation phenomenon is described. To track liquid-vapor interface, the volume of fluid multiphase model based on the piecewise linear interface construction method in curvilinear coordinate is used. A finite volume method code based on the SIMPLE algorithm and non-orthogonal discretization grid system is used for solving the governing equations including continuity, energy, and Reynolds averaged Navier-Stokes equations with the k-ε turbulence model. Also, the energy and mass transfer during the phase change is taken into account. The effects of inlet mass flow rate and temperature difference between the tube temperature and the saturation temperature on the local and average heat transfer coefficient and the net vapor production are presented. Results show the average heat transfer coefficient increases/decreases by increasing in the inlet mass flow rate/the temperature difference at a constant temperature difference/inlet mass flow rate. Results also demonstrate at a constant value of DT= _ m f (MED-TVC design approach), as the inlet mass flow rate increases, the heat transfer coefficient may be decreased or increased. This increase or decrease depends on the values of DT= _ m f and ΔT.

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Section: Introductionmentioning

confidence: 99%

Two-phase flow numerical simulation and experimental verification of falling film evaporation on a horizontal tube bundle

Bigham

Kouhikamali

Abadi

2014

Desalination and Water Treatment

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“…The heat transfer coefficients were found scatter among tubes from top to bottom with no significant discrepancy on any individual tube. This work was later extended by Habert [14]. Through his experimental study for plain tubes, similar scatter of heat transfer coefficient among tubes were obtained except tube 4 and 5 for higher heat transfer coefficient.…”

Section: Introductionmentioning

confidence: 57%

Characteristic study of steam maldistribution in horizontal-tube falling film evaporators

Shen

Gong

Liu

et al. 2015

Applied Thermal Engineering

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“…Correlations were developed to predict the heat transfer coefficients and the enhanced tubes had overall heat transfer coefficients of roughly twice those of the plain tube. Thome and co-workers [23,24] also conducted experiments to explore heat transfer performance on enhanced tube bundles using R-134a and R-236fa as the working fluid for all tubes bundles. They provided a new general method for predicting the onset of dryout on plain and enhanced tubes and proposed a general format for predicting local performance on a single row and on a tube bundle [25].…”

Section: Introductionmentioning

confidence: 99%

Heat Transfer Performance for a Falling-Film on Horizontal Flat Tubes

Wang

Hrnjak

Elbel

et al. 2013

Journal of Heat Transfer

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Local and average heat transfer behavior for a falling film on horizontal flat tubes is explored through an experimental approach. Experiments are conducted using water, ethylene glycol. and their mixture (50% by volume) under different heat fluxes and tube spacing, with a range of flow rates that covers all flow modes. It is found that the local heat transfer coefficient decreases with distance from the top of the tube. The distribution of the heat transfer coefficient along the axial direction depends on the flow mode: it is constant for the sheet mode, shows small variations for the jet mode, and has variations as large as 20% for the droplet mode. Heat flux has almost no effect on the average Nusselt number within the experimental range. The average Nusselt number for the flat tube is close to that for round tubes in the droplet flow mode, however, in the jet and sheet modes the flat-tube Nusselt number is much larger than the round-tube Nusselt number. Boundary-layer theory is used to explain the local heat transfer coefficient distribution and the experimental data show good agreement with the boundary-layer theory for most cases. New curve fits for the average heat transfer coefficient for three flow modes at different tube spacing are provided and the maximum deviation of the data from the fit is less than 14%.

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Falling-Film Evaporation on Tube Bundle with Plain and Enhanced Tubes—Part I: Experimental Results

Cited by 56 publications

References 13 publications

Two-phase flow numerical simulation and experimental verification of falling film evaporation on a horizontal tube bundle

Two-phase flow numerical simulation and experimental verification of falling film evaporation on a horizontal tube bundle

Characteristic study of steam maldistribution in horizontal-tube falling film evaporators

Heat Transfer Performance for a Falling-Film on Horizontal Flat Tubes

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