scholarly journals Drying Process Analysis of the Decreasing Drying Rate Period of Granular and Powder Material

1959 ◽  
Vol 23 (10) ◽  
pp. 641-647 ◽  
Author(s):  
R. Toei ◽  
S. Hayashi ◽  
T. Naito ◽  
M. Okazaki ◽  
M. Agata
Keyword(s):  
Powder Material ◽  
Process Analysis ◽  
Drying Rate ◽  
Drying Process ◽  
Rate Period

scholarly journals İncirin Sıcak Hava ve Mikrodalga Destekli Köpük Kurutma Yöntemi ile Kurutulması

2019 ◽  
Vol 7 (2) ◽  
pp. 291
Author(s):  
Mehmet Koç ◽  
Feyza Elmas ◽  
Emine Varhan
Keyword(s):  
Diffusion Coefficient ◽  
Effective Diffusion ◽  
Microwave Drying ◽  
Drying Rate ◽  
Drying Process ◽  
Hot Air Drying ◽  
Air Drying ◽  
Hot Air ◽  
Rate Period ◽  
Foam Thickness

In this study, the drying process of fig foam was carried out with hot air (60, 70, 80°C) and microwave (100, 300, 600 W) and the effect of drying process parameters and foam thickness on drying kinetics was investigated. The drying process was carried out only falling drying rate period and no constant drying rate period was observed. The drying times of the microwave drying were lower than the drying times of hot air drying due to the volumetric heating in addition to the large evaporation area on the foam surfaces. Drying times were shortened by increasing the temperature and microwave power whereas drying time increased with increasing foam thickness. Experimental drying data were placed in semi-empirical models of the 2. Fick's diffusion equation to determine kinetic parameters. Among them, it was found that Wang and Singh and Logarithmic models were better fitted for microwave and hot air drying respectively. The effective diffusion coefficient values for microwave and hot air drying varied between 9.94×10-10-405.69×10-10, 13.26×10-10-26.65×10-10 m2·s-1, respectively. Effective diffusion coefficient values increased with increasing temperature, microwave power and foam thickness. High thickness supported the diffusion process by convection of heat due to the increase in gaps in the structure. Activation energy which calculated with Arrhenius equation was varied from 2.195-2.379 W·g-1 for microwave drying and 12.952-21.426 kJ·mol-1 for hot air drying.

Drying of Industrial Ceramic Bricks: An Experimental Investigation in Oven

2014 ◽  
Vol 353 ◽  
pp. 116-120 ◽  
Author(s):  
G. Silva Almeida ◽  
M.A.F. Barbosa Fernandes ◽  
J.N. Ferreira Fernandes ◽  
Gelmires Araújo Neves ◽  
W.M.P. Barbosa de Lima ◽  
...  
Keyword(s):  
Experimental Study ◽  
Experimental Investigation ◽  
Atmospheric Pressure ◽  
Experimental Tests ◽  
Drying Rate ◽  
Drying Process ◽  
Clay Brick ◽  
Constant Weight ◽  
Rate Period ◽  
Temperature Constant

The purpose of this paper is to present an experimental study of clay brick drying. For the drying experiments, industrial holed bricks were dried in an oven under controlled conditions of velocity, temperature (constant and variable) and relative humidity of air. The continuous drying experiments ended when the mass reached constant weight. Experimental tests were performed under atmospheric pressure. Results of the drying and heating kinetics and volume variations during the process are shown and analyzed. It was verified that the drying process happens in the falling drying rate period, and air temperature has large influence in the drying rate during process. It was verified that the largest temperature, moisture content and stress gradients are located in the vertexes of the brick.

scholarly journals Experimental investigation of drying of malt bagasse

2018 ◽  
Author(s):  
G. S. Rosa ◽  
B. D. Zorzi ◽  
K. Machry ◽  
P. Krolow ◽  
C. M. Moura ◽  
...  
Keyword(s):  
Methylene Blue ◽  
Dye Removal ◽  
Adsorption Process ◽  
Fixed Bed ◽  
Experimental System ◽  
Operating Conditions ◽  
Convective Drying ◽  
Drying Rate ◽  
Drying Process ◽  
Rate Period

The aim of this work was to investigate the convective drying process of malt bagasse and to evaluate the influence of this process on the application of this residue as adsorbent in methylene blue removel by adsorption process. The experimental system for drying was a fixed bed dryer with parallel airflow, with operating conditions: air temperature in the range of 40 to 90 oC and air veocity of 2 m/s. The adsorption experiments were perfomed with solution of methylene blue at 70 ppm concentration. The drying kinetics showed a constant drying rate period followed by a falling drying rate. The results obtained for the dye removal efficiency were 56% for in natura sample and in the range of 81.69% to 93.99% for dried samples.Keywords: dryin; malt bagasse; adsorption

Heat and Mass Transfer and Volume Variations during Drying of Industrial Ceramic Bricks: An Experimental Investigation

2012 ◽  
Vol 326-328 ◽  
pp. 267-272 ◽  
Author(s):  
J. Barbosa da Silva ◽  
G. Silva Almeida ◽  
Gelmires Araújo Neves ◽  
W.C.P. Barbosa de Lima ◽  
Severino Rodrigues de Farias Neto ◽  
...  
Keyword(s):  
Experimental Study ◽  
Moisture Content ◽  
Air Temperature ◽  
Atmospheric Pressure ◽  
Drying Rate ◽  
Drying Process ◽  
Air Velocity ◽  
Brick Clay ◽  
Constant Weight ◽  
Rate Period

The purpose of this paper is to present an experimental study of brick drying. For the drying experiments, industrial brick (clay) was dried in an oven under controlled conditions of air velocity, air temperature and air relative humidity. The continuous drying experiments ended when the mass reached constant weight. In order, to obtain the balanced moisture content, each sample was kept under the same drying air temperature for 48 hours inside the oven. The tests were performed under atmospheric pressure. Results of the drying and heating kinetics and volume variations during the process are shown and analyzed. It was verified that air temperature has big influence in the drying rate during process. It was verified that the largest temperature, moisture content and stress gradients are located in the vertexes of the brick. The drying process happens in the falling drying rate period.

CATFISH DRYING (Clarias Batraclus) USING ‘TEKO BERSAYAP’ SOLAR DRYER

2012 ◽  
Vol 2 (1) ◽  
pp. 14-20
Author(s):  
Yuwana Yuwana
Keyword(s):  
Relative Humidity ◽  
Moisture Content ◽  
Ambient Temperature ◽  
Drying Rate ◽  
Drying Process ◽  
Drying Time ◽  
Ambient Relative Humidity ◽  
Solar Dryer

Experiment on catfish drying employing ‘Teko Bersayap’ solar dryer was conducted. The result of the experiment indicated that the dryer was able to increase ambient temperature up to 44% and decrease ambient relative humidity up to 103%. Fish drying process followed equations : KAu = 74,94 e-0,03t for unsplitted fish and KAb = 79,25 e-0,09t for splitted fish, where KAu = moisture content of unsplitted fish (%), KAb = moisture content of splitted fish (%), t = drying time. Drying of unsplitted fish finished in 43.995 hours while drying of split fish completed in 15.29 hours. Splitting the fish increased 2,877 times drying rate.

scholarly journals Effect of needle number on drying rate of kiwi fruit in EHD drying process

2013 ◽  
Vol 04 (01) ◽  
pp. 1-5 ◽  
Author(s):  
Mohammad Jafar Dalvand ◽  
Seyed Saeid Mohtasebi ◽  
Shahin Rafiee
Keyword(s):  
Drying Rate ◽  
Drying Process ◽  
Kiwi Fruit

scholarly journals Mathematical models to describe the drying process of Moringa oleifera leaves in a convective-air dryer

2021 ◽  
Author(s):  
Kivaandra Dayaa Rao Ramarao ◽  
Zuliana Razali ◽  
Chandran Somasundram
Keyword(s):  
Activation Energy ◽  
Mathematical Models ◽  
Moringa Oleifera ◽  
Effective Diffusivity ◽  
Drying Process ◽  
Constant Rate ◽  
Rate Period ◽  
Moringa Oleifera Leaves ◽  
Air Dryer ◽  
Kinetics Of

Drying kinetics of Malaysian Moringa oleifera leaves was investigated using a convective-air dryer. The drying parameters were: temperature (40, 50, 60, 70 °C), air velocity (1.3 m s<sup>–1</sup>, 1.7 m s<sup>–1</sup>). The drying process took place in the falling rate period and there was an absence of a constant rate period in this experiment. Six mathematical models (Lewis, Henderson and Pabis, Wang and Singh, Peleg, Page, and logarithmic) were selected for the description of drying characteristics of the leaves. The Wang and Singh model was determined as the best model based on the highest overall coefficient determinant (R<sup>2</sup>) and the lowest overall root mean square error (RMSE). The effective diffusivity (D<sub>eff</sub><sub> </sub>) was also calculated which was in the range of 3.98 × 10<sup>–11</sup> m<sup>2</sup> s<sup>–1</sup> to 1.74 × 10<sup>–10</sup> m<sup>2</sup> s<sup>–1. </sup>An Arrhenius relation was constructed to determine the activation energy for the samples in the convective air dryer. The activation energy for M. oleifera leaves was 39.82 kJ mol<sup>–1</sup> and 33.13 kJ mol<sup>–1</sup> at drying velocities of 1.3 m s<sup>–1</sup> and 1.7 m s<sup>–1</sup>, respectively.

Effect of Pre-Treatment on the Drying Characteristics and Kinetics of Okra (Abelmoschus esculetus (L.) Moench) Slices

2009 ◽  
Vol 5 (2) ◽  
Author(s):  
Olajide Sobukola
Keyword(s):  
Air Temperature ◽  
Sample Thickness ◽  
Hot Water ◽  
Drying Rate ◽  
Diffusivity Coefficient ◽  
Drying Characteristics ◽  
Rate Period ◽  
Pretreatment Conditions ◽  
Air Dryer ◽  
Kinetics Of

The effects of air temperature (50, 60 and 70°C), sample thickness (2, 4 and 6mm) and pretreatment conditions (hot water blanching, 1 and 3% sodium metabisulphite solutions) on the drying characteristics and kinetics of okra were investigated using a convective hot air dryer at a flow rate of 1.5m/s. It was observed that pretreatment conditions, sample thickness and drying air temperature significantly (P<0.05) affected drying rate. Drying rate increases as temperature of drying air increases from 50 to 70°C. The drying curve for all experiments occurred in the falling rate period with no constant rate period. Three thin layer drying models (Page, modified Page I and Wang and Singh) were evaluated using coefficient of determination (R2), root mean square error (RMSE) and the reduced chi square (?2). The three models can appropriately describe the drying kinetics of okra slices considering the different experimental conditions. The effective diffusivity was determined using the Fick’s model and was observed to vary between 1.125x10-8 – 9.93x10-9m2/s and 1.165x10-8 – 7.131x10-9 m2/s for treated and untreated samples. The Arrhenius-type relationship describes the temperature dependence of diffusivity coefficient and was determined to be 16.749kJ/mol and 22.437kJ/mol for treated and untreated samples respectively.

Study on the Vacuum Drying Model of Perilla Leaf by Microwave Method

2014 ◽  
Vol 664 ◽  
pp. 433-436
Author(s):  
Jiang Chang ◽  
Feng Xu ◽  
Guang Hua Wu ◽  
Xiao Feng Fu ◽  
Guang Li ◽  
...  
Keyword(s):  
Water Content ◽  
Kinetics Model ◽  
Vacuum Drying ◽  
Drying Rate ◽  
Microwave Method ◽  
Drying Process ◽  
Leaf Production ◽  
Microwave Vacuum Drying ◽  
Drying Model

The drying rate is difficult to control for perilla leaf during the microwave vacuum drying process. Through scientific approaches, this paper made a research on the relationships between drying factors and drying rate, and established a kinetics model on microwave vacuum drying of perilla leaf. The model can predict the water content variations of perilla leaf during microwave vacuum drying, and provides a theory basis for packaging, storage and transportation for perilla leaf production.

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