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Research Papers: Evaporation, Boiling, and Condensation

Numerical Simulations of Heat and Mass Transfer Process of a Direct Evaporative Cooler From a Porous Layer

[+] Author and Article Information
Karima Sellami

Transfer Phenomena Laboratory,
University of Science and
Technology Houari Boumediene,
BP 32 Bab Ezzouar,
Algiers 16111, Algeria
e-mail: sellami_karima@yahoo.fr

M'barek Feddaoui

LGEMS Laboratory,
National School of Applied Sciences of Agadir,
University of Ibn Zohr,
B.P. 1136,
Agadir 80000, Morocco
e-mail: m.feddaoui@uiz.ac.ma

Nabila Labsi

RSNE Team, FMGP,
Transfer Phenomena Laboratory,
University of Science and Technology
Houari Boumediene,
BP 32 Bab Ezzouar,
Algiers 16111, Algeria
e-mail: nabilalabsi@yahoo.fr

Monssif Najim

LGEMS Laboratory,
National School of Applied Sciences of Agadir,
University of Ibn Zohr,
B.P. 1136,
Agadir 80000, Morocco
e-mail: monssif.najim@edu.uiz.ac.ma

Youb Khaled Benkahla

RSNE Team, FMGP,
Transfer Phenomena Laboratory,
University of Science and Technology Houari
Boumediene,
BP 32 Bab Ezzouar,
Algiers 16111, Algeria
e-mail: youbenkahla@yahoo.fr

1Corresponding author.

Contributed by the Heat Transfer Division of ASME for publication in the JOURNAL OF HEAT TRANSFER. Manuscript received July 2, 2018; final manuscript received March 11, 2019; published online May 14, 2019. Assoc. Editor: Guihua Tang.

J. Heat Transfer 141(7), 071501 (May 14, 2019) (10 pages) Paper No: HT-18-1424; doi: 10.1115/1.4043302 History: Received July 02, 2018; Revised March 11, 2019

This paper deals with the numerical study of the combined heat and mass exchanges in the process of direct evaporative cooler, from a porous media of laminar air flow between two parallel insulated walls. The numerical model implements momentum, energy, and mass conservation equations of humid air and water flow incorporating non-Darcian model in the porous region. The finite volume method is used for the mathematical model resolution, and the velocity–pressure coupling is treated with the SIMPLE algorithm. The main objective of this study is to examine the influences of ambient conditions and the porous medium properties (porosity and porous layer thickness) on the direct evaporative cooling performance from a porous layer. The major results of this study demonstrate that the porous evaporative wall could, in a satisfying manner, reduce the bulk air temperature. The better cooling performance can be achieved for lower air mass flow at the entrance and relative humidity. Additionally, the evaporative cooler is more effective for a high porosity and a thick porous medium, with an improvement achieving 23% for high porosity.

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Figures

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Fig. 1

Configuration of a direct evaporative cooler

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Fig. 2

Geometry scheme of the studied problem

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Fig. 3

Longitudinal variation of the interfacial dimensionless temperature (a) and the mass evaporation rate (b) for ε=0.8andd=0.01 m

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Fig. 4

Evolution of the temperature (a) and velocity (b) profiles at various sections for various humidities. TG0=35 °C,TL0=20 °C, mG0=40 kg m−1 h−1, ε=0.3, and d=10 mm.

Grahic Jump Location
Fig. 5

Axial evolution of temperature and humidity with the air mass flow (a) and humidity (b) variation at the entrance. TG0=35 °C, TL0=20 °C, ε=0.3, and d=10 mm.

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Fig. 6

Evolution of the sensible and latent heat flux exchanges versus the inlet air mass flow and humidity variations. TG0=35 °C, TL0=20 °C, ε=0.3, and d=10 mm.

Grahic Jump Location
Fig. 7

Evolution of the temperature (a) and velocity (b) profiles at various sections for various humidity. TG0=35 °C,TL0=20 °C,mG0=40 kg m−1 h−1, ϕ0=10%, and d=10 mm.

Grahic Jump Location
Fig. 8

Axial evolution of temperature and humidity with the variation of porous layer thickness (a) and porosity (b). TG0=35  °C, TL0=20 °C, ϕ0=10%, and mG0=40 kg h−1 m−1.

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Fig. 9

Evolution of the sensible (a) and latent (b) heat fluxes with the variation of porous media thickness and porosity. TG0=35 °C, TL0=20  °C, ϕ0=10%, and mG0=40 kg h−1 m−1.

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Fig. 10

System efficiency and cooling capacity variation versus the air inlet mass flow for various values of the water temperature and relative humidity. TG0=35 °C,ε=0.3, andd=10 mm.

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Fig. 11

System efficiency and cooling capacity with variation of the porosity. TG0=35 °C,mG0=40 kg h−1 m−1, andd=10 mm.

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Fig. 12

System efficiency and cooling capacity with variation of the porous media thickness. TG0=35 °C, ϕ0=10%,mG0=40 kg h−1 m−1, and d=10 mm.

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