drying strategies of fluidized bed dryer

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Drying Strategies for Fluidized-Bed Drying ofPaddy

Article in International Journal of Food Engineering January 2009

Impact Factor: 0.5 DOI: 10.2202/1556-3758.1401

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4 authors, including:

Supawan Tirawanichakul

Prince of Songkla University

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Somkiat Prachayawarakorn

King Mongkut's University of Technology Tho

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Dr. Warunee - Varanyanond

Kasetsart University

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Available from: Somkiat Prachayawarakorn

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International Journal of Food

Engineering

Volume5, Issue2 2009 Article6

Drying Strategies for Fluidized-Bed Drying of

Paddy

Supawan Tirawanichakul Somkiat Prachayawarakorn

Warunee Varanyanond Somchart Soponronnarit

Prince of Songkla University, [email protected]

King Mongkuts University of Technology Thonburi, [email protected] University, [email protected]

King Mongkuts University of Technology Thonburi, [email protected]

Copyright c2009 The Berkeley Electronic Press. All rights reserved.


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Drying Strategies for Fluidized-Bed Drying of

Paddy

Supawan Tirawanichakul, Somkiat Prachayawarakorn, Warunee Varanyanond,

and Somchart Soponronnarit

Abstract

The main objective of this work was to determine an effective moisture diffusivity of long

grain rice during fluidized-bed drying (FBD) with inlet drying temperatures ranging of 40-150

Cby 10C/step and to investigate the specific energy consumption of the FBD process. Three initial

moisture contents of the local indica paddy were set at 25.0, 28.8 and 32.5% dry-basis. The exper-

imental results of thin-layer fluidized-bed drying for the long grain rice variety were determined

and statistically analyzed by non-linear regression method. The results showed that an effective

diffusion coefficient was highly dependent on the drying temperature, compared to initial mois-

ture content. Consequently, the mathematical simulation of FBD, using the developed thin-layer

drying mentioned above, was evaluated and used for predicting the paddy drying system. The

simulated value of energy consumption in each of the drying conditions was comparatively sim-

ulated. The simulated results showed that a FBD with low temperatures and low initial moisture

content gave higher specific energy consumption than drying with high temperatures and high ini-

tial moisture contents. The total specific energy consumption increased with a decreased fraction

of re-circulated outlet drying air. According to the simulation results and our previous work, the

conclusion is that the long grain paddy drying with FBD technique under a high initial moisturecontent and drying air temperature over 100C is the good drying condition for recommendation.

KEYWORDS:effective diffusivity, energy consumption, long grain paddy, mathematical model-

ing, non-glutinous rice

The authors wish to express our sincere thanks to the Thailand Research Fund (TRF); the Japan

International Research Center for Agricultural Sciences (JIRCAS); the Institute of Food Researchand Product Development (IFRPD), Kasetsart University; the Department of Chemical Engineer-

ing, Faculty of Engineering, Department of Energy Technology, School of Energy Environment

and Materials, King Mongkuts University of Technology Thonburi; and the Department of Chem-

ical Engineering, Faculty of Engineering, Prince of Songkla University for their support and their

facilities.


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1. Introduction

Normally, fresh paddy after harvesting contains moisture content of 24-35% dry-

basis. The high moisture content paddy is easy to deteriorate, especially storage intropical climate surrounding. These moisture content values must be removed to

preserve the storage life of the grain (Quitco, 1982; Soponronnarit andNathakaranakule, 1990; Sutherland and Ghaly, 1990; Siebenmorgen et al., 1998;

Zhou et al., 2002; Tirawanichakul et al., 2003) and to reduce handling cost.

Drying is the most common forms of grain, cereal grain and food preservation. In

addition, drying provides long term storage and extends grain shelf life withoutdeterioration. Even a solar drying is regularly used for reducing moisture content

of fresh paddy but sometimes, it is difficult to practice in tropical areas during

rainy season period. Some researchers recommended that fresh paddy with amoisture content over 24% dry-basis should be first removed to 22% dry-basis

within 24 hours by the fast hot air drying (using high temperature with a shortdrying time) and then followed by natural air drying (using low temperature)(Driscoll and Adamczak, 1988; Soponronnarit et al., 1999; Poomsa-ad et al.,

2002). Thus, an force convection air drying such as the cross-flow dryer, spouted-

bed and fluidized-bed is an appropriate method to solve this problem because

drying time for high percentages of moisture removal is relatively short such asthe spouted-bed (Devahastin and Mujumdar, 2001) and fluidized-bed drying;

(Soponronnarit and Prachayawarakorn, 1994). The fluidized-bed drying is an

effective approach and of the main interest in this work. This is because a hot airfluidized-bed drying is one of the drying techniques that provides faster moisture

reduction and uniformity of drying. Consequently, this drying technique improves

the physical quality in terms of head rice yield and maintains some qualities(Tirawanichakul et al., 2004). However, many researchers were interested in

paddy FBD with inlet air temperature over 100C (Soponronnarit et al., 1996;Soponronnarit et al., 1999;Tirawanichakul et al., 2004). Despite of the popularity

of fluidized-bed dryer for paddy, there are a few reports concerning theoreticaldrying model using effective diffusivity and development of mathematical

fluidized-bed paddy drying model for predicting evolution of moisture transfer

and energy consumption covering wide ranges of drying temperature.Therefore, the aims of this research were to use the mathematical model

developed for continuous fluidized-bed paddy dryer to simulate drying kinetic of

paddy with various initial moisture contents of 25.0-32.5% dry-basis and to

determine the specific energy consumptions when the dryer is ideally operated atdifferent drying conditions. The effective diffusivity of paddy determined by non-

linear regression analysis was used in the theoretical thin-layer drying equation in

this simulation. Finally, comparative study between experimental data and

simulated data are presented.

1

Tirawanichakul et al.: Drying Strategies for Fluidized-Bed Drying of Paddy

Published by The Berkeley Electronic Press, 2009
https://www.researchgate.net/publication/237230801_Milled_Rice_Breakage_Due_to_Environmental_Conditions_1?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/222532880_Ageing_of_Stored_Rice_Changes_in_Chemical_and_Physical_Attributes?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/232829092_Experiments_on_In-Store_Paddy_Drying_Under_Tropical_Climate_Simulation_and_Product_Quality?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/232892806_Managing_moist_paddy_by_drying_tempering_and_ambient_air_ventilation?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/223683969_Some_hydrodynamic_and_mixing_characteristics_of_a_pulsed_spouted_bed_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244602845_Optimum_strategy_for_fluidized_bed_paddy_drying?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603239_Effect_of_Fluidized_Bed_Drying_Temperature_on_Various_Quality_Attributes_of_Paddy?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/232892806_Managing_moist_paddy_by_drying_tempering_and_ambient_air_ventilation?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603239_Effect_of_Fluidized_Bed_Drying_Temperature_on_Various_Quality_Attributes_of_Paddy?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/237230801_Milled_Rice_Breakage_Due_to_Environmental_Conditions_1?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/232829092_Experiments_on_In-Store_Paddy_Drying_Under_Tropical_Climate_Simulation_and_Product_Quality?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/223683969_Some_hydrodynamic_and_mixing_characteristics_of_a_pulsed_spouted_bed_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603239_Effect_of_Fluidized_Bed_Drying_Temperature_on_Various_Quality_Attributes_of_Paddy?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-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5/23

2. Materials and Methods

(A) Experimental procedure

The dryer comprised of a cylindrical shaped drying chamber, a 4x4 kW electric

heating unit and a backward curved blade centrifugal fan driven by a 1.5 kWmotor. The Suphanburi 1 (SP1) and Pathumthani 1 rice varieties (PT1) provided

by the Rice Research Institute (Pathumthani province), was used for this

experiment. The average initial moisture content of paddy was varied from 25.0 to

32.5% dry-basis. Fresh paddy was dried at the inlet drying air temperatures of

40C to 150C by 10C/step. A constant air velocity of 2.2 m/s was set up for thebed depth of 0.015 m. The inlet drying air temperature, outlet air temperature andambient air temperature were measured by K-typed thermocouple connected to a

data logger with an accuracy of 0.5C. The moisture contents of paddy weredetermined followed by AOAC method (AOAC, 1995). The experiments were

measured by means of triplication. These drying conditions were the same as the

previous work which dried samples were studied in terms of physical, chemical,physico-chemical and tasting analysis (Tirawanichakul et al., 2004).

(B) Development of moisture diffusion models

The moisture is actually transferred by liquid diffusion. Thus, in this work, the

assumption is that water moves out from paddy by liquid diffusion and the water

vapour moves out in the directions of radial and axial coordinates and finally, theshrinkage of paddy is negligible during the drying. The paddy kernel is an

isotropic solid and is in a form of short cylindrical shape (so-called as a finitecylinder). Thus, the partial differential equation of moisture diffusion for a singlepaddy kernel, considered geometrically as a finite cylindrical shape, can be

followed by the previous work (Crank, 1975) while an effective diffusioncoefficient (D) is namely described by the Arrhenius type equation as follows:

=

abs

a

RT

EexpDD (1)

whereD = the effective diffusivity accounting for the heterogeneous

solid, m2/h or m

2/s

Ea = the activated energy, kJ/kmol-KR = universal gas constant, kJ/kmol-K

Tabs = absolute temperature, K

2

International Journal of Food Engineering, Vol. 5 [2009], Iss. 2, Art. 6

http://www.bepress.com/ijfe/vol5/iss2/art6

DOI: 10.2202/1556-3758.1401
https://www.researchgate.net/publication/244603239_Effect_of_Fluidized_Bed_Drying_Temperature_on_Various_Quality_Attributes_of_Paddy?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/221658015_The_Mathematics_Of_Diffusion?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/221658015_The_Mathematics_Of_Diffusion?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603239_Effect_of_Fluidized_Bed_Drying_Temperature_on_Various_Quality_Attributes_of_Paddy?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==


6/23

and D is the Arrhenius factor and depends on the drying air temperature and themoisture content or a constant value (Hebber and Rastogi, 2001). Some previous

researchers also reported that the Arrhenius factor (D ) was in the form of thesecond order polynomial in relation with moisture content of paddy kernel. TheD and Eavalues were determined by the non-linear regression analysis from theexperimental data.

(C) Mathematical model

Considering the energy analysis of continuous fluidized-bed dryer, a schematicdiagram of a fluidized-bed dryer was illustrated in Figure 1. The assumptions of

the mathematical model of a continuous fluidized-bed drying are in the thermal

equilibrium between moist air and paddy, the walls of dryer are adiabatic, themoisture is transferred by liquid diffusion and the shrinkage is negligible during

the drying. The flow chart of calculation procedure is shown in Figure 2. Amathematical model for predicting the moisture reduction and temperature in this

work was corresponded to that previously described by Soponronnarit et al.,(1996). The derivations of energy and mass equations are written based on basic

physical laws.

(1) Basic parameters of continuous fluidized-bed drying

Mean residence time is defined as the time which paddy stays in drying chamberuntil it leaves from it, is calculated by the following equation

F

upHold = (2)

where

= mean residence time, minF = feed rate of paddy, kg/minHold up = mass of fresh paddy in drying chamber, kg and the hold

up can be calculated as follows

Hold up = (AC)(pw))(Hi) (3)

where

AC = cross section area of drying chamber, m2

pw = density of paddy, kg/m3

Hi = height of weir, m

3


https://www.researchgate.net/publication/222525678_Mass_transfer_during_IR_drying_of_cashew_kernel?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/283763164_Development_of_cross-flow_fluidized_bed_paddy_dryer?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/222525678_Mass_transfer_during_IR_drying_of_cashew_kernel?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==


7/23

In this present work, the model of continuous fluidized-bed is composed of

series of thin layers. As shown in control volume 1(CV1), the paddy bed in drying

chamber is horizontally divided into n layers.

n

t = (4)

Air mass flow rate at the ith

layer is given by

n

mm mixmixi

&& = (5)

and holdup of paddy is also written as:

n

hphp i = (6)

where

t = time used for moving from the ith

layer to the (i+1)th

layer, min

hpi = dry mass of paddy at the ith

layer, kg

mixm& = air mass flow rate, kg/min

mixim& = air mass flow rate at the ith

layer, kg/min

n = number of layer for paddy

A mathematical model for predicting the evolution of moisture transfer and

temperature profile in this work was similar to that previously described by

Soponronnarit et al., (1992). The derivations of energy and mass equations are

written based on basic physical laws. The analytical solution for the moistureinside a single kernel is expressed by the following equation (Crank, 1975).

The initial and boundary conditions for fluidized-bed paddy drying are

given by

t = 0, 0r r0 M = Minll + z M = Min

t > 0, r = r0 M = Meq

l=z M = Meq

t > 0, r = 0 0r

M=

4



DOI: 10.2202/1556-3758.1401
https://www.researchgate.net/publication/221658015_The_Mathematics_Of_Diffusion?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/221658015_The_Mathematics_Of_Diffusion?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==


8/23

2eq m

0 m2 2m 1in eq 0m 1 m 0

M(r,l,t)-M Dt4 2 rMR(r,l, t) J exp

M - M r J ( ) r

=

= =

=

+++0n

22n

l4

Dt1)n(2-exp

l2

z1)n(2cos

1n2

(-1) (7)

whereMR = moisture ratio, decimal

t = drying time, h or s

m = root of the Bessel function of the nth

kind of zero order

r = radius of the cylinder material, m

z = height of the cylinder material, m

l = half length of cylinder, m

M = moisture content at any time t, decimal (dry-basis)Min = initial moisture content, decimal (dry-basis)

n = number of layer for paddy

The equilibrium moisture content (EMC, Meq) for paddy was modified in

form of Hendersons equation (Henderson, 1952). By integrating of Eqn.(7) overthe volume of cylinder and dividing by its total volume, the average moisture

content can be expressed as:

( )

+

+

=

=

= l4

Dt1)n(2exp

1n2

1

r

Dtexp

4

8MR

22

0n22

o

2

m

1m2

m

2 (8)

(2) Energy conservation of drying chamber

Considering a given thin layer drying, the energy equation is derived based on thefirst law of Thermodynamics. It is assumed that the flow of paddy in drying

chamber is the plug flow type and uniform hot air flow passing though each

paddy layer is considered. As shown in Figure 1 for the control volume CV1,

change of enthalpy of air and internal energy change of paddy and dryingchamber are equal to total heat transfer between drying chamber and environment.

To determine the outlet air temperature from the ith

drying layer, the following

equation can be written as:

pfifivfgfiamixmixvfgmixamixi1 u)WTc(hTc)WTc(hTcm/Q +++=+++& (9)

or

5




9/23

)cW]/(cu)h(W)WTc(hTcm/Q[T vfiapfgfimixmixvfgmixamixi1fi ++++= & (10)

and

T)UA(Q1 = (11)

where

ca = specific heat of dry air, kJ/kg-Ccv = specific heat of water vapour, kJ/kg-Chfg = latent heat of vaporization of water, kJ/kg-water

Q1 = heat losses from control volume CV1 to surrounding,kW

U = overall heat transfer coefficient, kW/m2-C

A = surface area of system (CV1), m2T = temperature difference between system (CV1) and

surrounding, CTfi = outlet air temperature at the i

thlayer, C

up = change of internal energy of paddy per unit mass of dryair, kJ/ kg-dry air

Wfi = humidity ratio of air at the ith

layer, kg-water/kg-dry air

Wmixi = humidity ratio of air at the ith

layer, kg-water/kg-dry air

(3) Mass conservation at drying chamber

In a small time interval of t, a certain amount of moisture evaporates from thegrain bed at the i

thlayer into the air, resulting in a change of the humidity ratio of

inlet air. The equation of mass balance can thus be written as

ihp)M(Mtm)W(W fiimiximixfi = &

or

mix

imixi

1iiifi W

]tm[

)M(MhpW +

= +

& (12)

where

Wfi = outlet humidity ratio of air, kg water/kg dry airWi = inlet humidity ratio of air, kg water/kg dry air

6



DOI: 10.2202/1556-3758.1401


10/23

Mi = average moisture content at time = t, decimal (dry-basis)

Mf = average moisture content at time = t+t, decimal (dry-basis)

mp = dry mass of sample, kg

ti = drying time of paddy in the ith

layer

Finally, the average outlet temperature and humidity ratio of exit air can be

determined by Eqns.(13) and (14), respectively.

=

n

0

n

1

fi

f1

dn

dnT

T (13)

=

n

1

n

1

fi

f1

dn

dnW

W (14)

where

f1T = average outlet temperature at drying chamber exit, C

f1W = average outlet humidity ratio at drying chamber exit,

decimal

(4) Energy conservation at recycle tube

As illustrated in control volume CV2 in Figure 1, the outlet temperature from

recycle tube can be calculated by balancing the change of enthalpy of air streamand summation of heat exchange between recycled air and environment. The

following equation of exit temperature at recycle tube is given by:

)cW(c

)T(cWTcm(RC)

Q

Tvfia

fivfifia

mix

2

f2 +

++

=&

(15)

where

Tf2 = air temperature at recycle tube exit, C

7




11/23

RC = fraction of recycled air, decimal

RCm& = dry mass flow rate of recycled air, kg/s

Q2 = rate of heat loss from control volume CV2 tosurrounding, kJ/s

A = surface area of recycle tube, m2

(5) Mass conservation before fan entrance

To determine the humidity ratio after mixing between fresh air and recycled air asshown in Figure 1, the conservation of mass is made with control volume CV4 in

which amount of water vapour after mixing is equal to the summation of water

vapour from fresh air stream and recycled air. The mass balance equation for

water vapour can be written as follows:

mixiRCiifRC )Wmm(WmWm &&&& +=+ (16)

Finally, dry mass flow rate of inlet drying air at drying chamber entrance is

equal to the summation of dry mass flow rate of fresh air and recycled air. Thus,

the following equation is written as

iRCmix mmm &&& += (17)

From Eqns.(16) and (17), the humidity ratios after mixing between recycledair and fresh air is determined by:

fiimix RCWRC)W(1W += (18)

where

RC =mix

RC

m

m

&

& (19)

(6) Energy consumption of system

(a) Temperature of air at fan entrance

The energy balance is applied for CV4 to determine the temperature after mixing

between the recycled air and fresh air, thus yielding:

8



DOI: 10.2202/1556-3758.1401


12/23

0)Tc(hWm-Tcm

)Tc(hWm-Tcm-)Tc(hWmTcm

f2vfgf1rcf2arc

ivfgiiiaixvfgmixmixxamix

=+

+++

&&

&&&&

(20)

and

Tb = Tx+Tfan (21)

where

Tb = outlet temperature of air stream at fan exit, CTx = mixed temperature of air before fan entrance, CTfan = temperature rise of air while flowing across a fan, CTi = ambient air temperature, C

(b) Temperature rise of air at fan

The energy balance is applied for CV4 to determine the temperature after mixing

between the recycled air and fresh air as follows:

)]Wc)(cE[1000(

PT

mixvafafan +

= (22)

where

a = air density, kg/m3

P = pressure drop across the fan, kPa

Ef = fan efficiency (0.5), decimal

Electrical energy consumption of fan is determined from pressure drop in

recycle tube, pressure drop at exit tube and pressure drop at paddy bed in dryingchamber. These following equations are followed by Soponronnarit (1997):

Pressure drop at tubes is written as:

250m13.1006)(10.534RCP 2mix2

L ++= & (23)

Pressure drop at paddy bed is found:

=

capB

g

g)-)(-H(1P (24)

where

9




13/23

PL = pressure drop at recycle tubes, respectively; Pa

RC = recycled air ratio, decimal

PB = pressure drop across paddy bed, Pa

H = weir of paddy in drying chamber, m

= spacing ratio of paddy in drying chamber, decimalp = density of air, kg/m

3

a = apparent density of paddy kg/m3

g = local gravitational constant, m/s2

gc = gravitational constant of earth, m/s2

Total pressure drop of drying system (Pt) composes of pressure drop inrecycled tube, pressure drop at exit tube, pressure drop at perforated sheet

(assuming that 30% of pressure drop of grain bed) and pressure drop cross the

grain bed. The expression of total pressure in drying is then given by

1000

)1.3P(PP BLt

+= (25)

where

Pt = total pressure loss of system, kPa

Thus, the shaft power for driving fan can be calculated by the followingequation:

m

t

E)P(q)(BP = (26)

whereBP = shaft power, kW

q = volumetric air flow rate, m3/s

Em = mechanical efficiency, decimal

(c) Energy consumption of heating unit

As shown in the control volume CV3 in Figure 1, the change of enthalpy of airstream is equal to heat loss and supplemental heat from electrical heater. The

equation can be written as follows:

( )[ ]( )bmixmixvamixh3 TTWccmQQ +=+ & (27)

10



DOI: 10.2202/1556-3758.1401


14/23

where

Qh = electrical energy consumption of heater, kJ/s or kW

Q3 = heat loss at heating unit, kJ/s or kW

Considering a given thin layer drying, the energy equation is derived based

on the first law of Thermodynamics. It is assumed that the flow of paddy in

drying chamber is the plug flow type and uniform hot air flow passing thougheach paddy layer is considered. For the control volume CV1 as shown in Figure 1,

change of enthalpy of air and internal energy change of paddy and drying

chamber are equal to total heat transfer between drying chamber and environmentand determining of the outlet air temperature from the i

th drying layer can be

achieved. In a small time interval of t, a certain amount of moisture evaporatesfrom the grain bed at the i

thlayer into the air, resulting in a change of the humidity

ratio of inlet air can be determined from equation of mass balance. Finally, theaverage outlet temperature of exit air can be determined by integration of productof final temperature and number of layer dividing by total number of layers as the

same as calculating of average humidity ratio of outlet air.

As illustrated in control volume CV2 in Figure 1, the outlet temperaturefrom recycle tube can be calculated by balancing the change of enthalpy of air

stream and summation of heat exchange between recycled air and environment

whilst determining the humidity ratio after mixing between fresh air and recycled

air also can be calculated by the mass balance equation for water vapour incontrol volume CV4 (Figure 1). Finally, dry mass flow rate of inlet drying air at

drying chamber entrance is equal to the summation of dry mass flow rate of fresh

air and recycled air and the humidity ratios after mixing between recycled air andfresh air is determined. In addition, the energy balance is applied for control

volume CV4 to determine the temperature after mixing between the recycled airand fresh air.

Electrical energy consumption of fan is determined from pressure drop in

recycle tube, pressure drop at exit tube and pressure drop at paddy bed in dryingchamber, following to Tirawanichakul (2004). As shown in the control volume

CV3, the change of enthalpy of air stream is equal to heat loss and supplemental

heat from electrical heater. To compare energy consumption among different inlet

drying air temperature, the specific energy consumption of this fluidization isconsidered. The specific energy consumption for each drying condition is defined

as energy consumption divided by total water evaporated and multiplied bydrying time. The total specific energy consumption is a summation of specificthermal energy consumption and specific electrical energy consumption

multiplied by total drying time. In the mathematical modeling, assumption is

11




15/23

stated that the continuous fluidized-bed drying was used for drying paddy at the

temperatures between 60 and 150C using inlet air velocity of 2.5 m/s and thefraction of recycled air was varied between 0 and 95%. Initial moisture contents

of 25.0%, 28.8% and 32.5% dry-basis were dried to 22.50.5% dry-basis.Ambient temperature was fixed at the condition of dry bulb temperature of 30Cand relative humidity of 70%.

3. Results and discussions

(A) Determination of effective diffusivity

Table 1 shows the determination of constant values in two diffusion models using

non-linear regression analysis among inlet drying air temperatures of 40-150C

and initial moisture contents of 22-32.5% dry-basis The diffusion Model 1 andModel 2 have the activation energy of -37099 kJ/mol and -40904.79 kJ/mol,respectively as shown in Eqns. (28) and (29), respectively. The result indicates

that the Arrhenius factor (D ) for Model 1 is determined as 4.33x10-5 m2/s [or2600 mm

2/min] whilst the Arrhenius factor for Model 2 depends on initial

moisture content for example: 2.0x10-4

m2/s for the initial moisture content of

25% dry-basis. The correlation coefficient (r2) for both of equations is about 0.9

while the mean residue square value (MRS) for Model 1 and Model 2 are 0.005

and 0.001, respectively. The results indicate that the mean residual square value(MRS) for Model 2 has a high accuracy comparing to that of Model 1. From the

evolution of moisture content throughout the drying time at different inlet drying

air temperatures (40C-150C) of simulated and measured values for Model 1 andfor Model 2, all drying curves of these figures clearly show that drying rates ofpaddy are in the falling rate period. The results show that the simulated resultsusing both of diffusion coefficients for Model 1 and Model 2 are also in good

agreement with the experimental results. However, the predicted values using the

diffusion Model 2 are slightly close to experimental values, comparing to the

predicted values using the diffusion Model 1. By non-linear regression technique,it indicated that the effective diffusion coefficient strongly depended on the inletdrying air temperature and was slightly related to the initial moisture content of

paddy as shown in Table 1. Thus, drying time at the high drying air temperature,

which has a high diffusivity, was shorter than that of drying at the low drying air

temperature.

12



DOI: 10.2202/1556-3758.1401


16/23

(B) Validation of mathematical drying model

To verify the mathematical model proposed, the experimental results from

previous works (Poomsa-ad et al., 2002) were used and the calculated results werepresented in Table 2(a)-2(c).

Feed rate of paddy was set-up between 3.12 and 6.42 ton/h. The initialmoisture content and final moisture content of paddy was in range of 24.1 to

28.0% dry-basis and 20.4 to 22.5 % dry-basis, respectively. The results show that

the proposed model can predict the final moisture content and energy

consumptions at various drying conditions in good agreement with theexperimental results.

To comparative study of specific energy consumption, the predicted values

of thermal and electrical energy for the continuous fluidized-bed dryer operated at

inlet temperatures of 60C to 150C in various initial moisture contents andfractions of air recycled were determined. Tables 3 and 4 are example of predicted

data under the drying air temperature of 60C and 150C, respectively. Theresults show that the specific total energy consumption for drying paddy at lowtemperature is relatively high as compared to drying with high temperature. The

energy largely consumed is a main part of electrical power for driving fan since

low temperature drying takes longer operating time. Consequently, the predictedvalues of the specific total energy consumption for drying paddy at initial

moisture content of 25.0% dry-basis are higher than that of initial moisture

contents of 28.8 and 32.5% dry-basis. This is because the moisture content at the

lower initial moisture content is in intercellular so it is more difficult to transferfrom paddy kernel to the air. Due to effect of fraction of recycled air on total

specific energy consumption, it shows that the predicted values of specific totalenergy consumption for drying paddy at initial moisture content of 25.0, 28.8 and32.5% dry-basis are in the range of 20.01 to 24.37 MJ/kg of water evaporated for

the fluidized-bed operated with no air recycle and 8.92 to 11.99 MJ/kg of waterevaporated for the fraction of recycled air of 90%. However, as the drying

temperature is increased, the total specific energy consumption is decreased with

the minimum energy required being at temperature of 150C. At this temperaturethe total specific energy consumption for the case of no air recycle is in the range

of 7.49 to 11.37 MJ/kg of water evaporated for drying paddy at initial moisturecontents of 25.0, 28.8 and 32.5% dry-basis, with the lowest energy for the

moisture content of 32.5% dry-basis. Besides the temperature effect, the total

specific energy consumption is decreased with increased fraction of air recycle,90% of recycled air suitable for operating the fluidized-bed dryer. Under such

operating conditions, 150C and 90% of air recycle, the total specific energyconsumptions were 7.02, 5.49 and 4.70 MJ/kg of water evaporated for the

respective moisture contents of 25.0, 28.8 and 32.5%. From the predicted results

13


https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==https://www.researchgate.net/publication/244603087_Effect_of_tempering_on_subsequent_drying_of_paddy_using_fluidisation_technique?el=1_x_8&enrichId=rgreq-d97ce0d6-11b1-4dbc-a8ed-4495c855d99f&enrichSource=Y292ZXJQYWdlOzI1MDE0NzQ2MTtBUzoyMDg4NzkxMjUzMDczOTNAMTQyNjgxMjA3MjI0MA==


17/23

aforementioned above, they indicate that the operation of fluidized-bed at the inlet

air temperature below 100C is not be suitable for commercial point of viewbecause it takes long time for drying paddy and the specific total energy

consumption is relatively high. Moreover, to determine effect of drying

temperature and moisture content of paddy, the previous work of our research hasbeen presented (Tirawanichakul et al., 2004) and the results showed that the head

rice yield of Suphanburi 1 rice variety was significantly related to the inlet drying

temperature and initial moisture content whilst there was no significantly relationbetween the head rice yield, drying temperatures and initial moisture contents for

Pathumthani 1 rice variety. The whiteness value of the two rice varieties was

slightly decreased with increase in drying temperature and initial moisture

content. However, for all experiments, the whiteness values were within anacceptable range for the commercial purpose (Soponronnarit et al., 1999). For

determining taste analysis, the hardness value of both cooked rice varieties

exhibited insignificant difference (p


18/23

Electric heater

Recycled air

Exhaust air

addy bed

Perforated steel

Fan

Inlet air

CV1

CV3

CV4

CV5

CV2

Tf2

Wf1

Q1

Q2

Q3

Tf1

Wi, Ti

Tx

Tb

Tmix

Figure 1 Schematic diagram of a fluidized-bed dryer with recycle pipe

15




19/23

Start

INPUT DATA: v, F, RC, H, mmix, Tmix, Ti, Twb, Mi

CAULATE : mean residence time

CALCULATE: t,mmixi, hold up (hpi)

Wf1, assume = 002

CALCULATE: Wfi, Tfi, Mfi

For i > n

CALCULATE: Tf1, Wf1

Check Wf1

CALCULATE: Energy consumption

End

Wf1,assume = Wf1

NO

YES

YES

NO

StartStart

INPUT DATA: v, F, RC, H, mmix, Tmix, Ti, Twb, Mi

CAULATE : mean residence time

CALCULATE: t,mmixi, hold up (hpi)

Wf1, assume = 002

CALCULATE: Wfi, Tfi, Mfi

For i > n

CALCULATE: Tf1, Wf1

Check Wf1

CALCULATE: Energy consumption

End

Wf1,assume = Wf1

NO

YES

YES

NO

Figure 2 Simulation flow chart of fluidized-bed drying

16



DOI: 10.2202/1556-3758.1401


20/23

Table 1 Diffusivity function of paddy drying by fluidized-bed technique using

inlet drying temperatures of 40-150C and initial moisture content (Min)ranging of 22.0-32.5% dry-basis

Model Effective diffusion model r2 MRS*

1

=

absRT

37099-exp2600D

(28)

0.93 0.005

2

+

=

abs

in

2

in

RT

40904.79-exp13999.99)

M4209.99M(1.18D

(29)

0.97 0.001

Note: *Mean residue square value was calculated as follows:,

N

)MR(MR

MRS

2

iobserved,

N

1i

iPredicted, =

=

17




21/23

Table 2 Comparison between experimental and predicted results of continuous

fluidized-bed drying using inlet drying temperatures of 130-150C.(a) Moisture content

RunNo.

Drying

Temperature (C)Feed rate(ton/h)

Bed height(m)

Min(% dry-

basis)

Mf(% dry-basis)Exp.1 Sim2

1 130 3.12 0.115 25.9 22.5 22.5

2 130 4.82 0.115 26.8 23.7 24.0

3 140 4.72 0.147 26.7 23.3 23.1

4 140 4.82 0.115 24.1 20.7 20.5

5 150 6.42 0.119 25.9 23.3 23.2

6 150 6.09 0.150 25.9 23.7 23.2

7 150 5.10 0.150 26.1 23.4 22.8

8 150 4.82 0.115 28.0 23.0 23.6

(b)

Specific thermal energy consumption (STEC)

Run

No.

Drying

Temperature

(C)

Feed rate

(ton/h)

Bed height

(m)

Min

(% dry-

basis)

STEC

(MJ/kg of water

evaporated)

Exp1 Sim2

1 130 3.12 0.115 25.9 6.45 5.82

2 130 4.82 0.115 26.8 5.47 5.88

3 140 4.72 0.147 26.7 4.83 4.88

4 140 4.82 0.115 24.1 4.69 5.02

5 150 6.42 0.119 25.9 4.93 5.11

6 150 6.09 0.150 25.9 6.70 7.72

7 150 5.10 0.150 26.1 6.01 5.668 150 4.82 0.115 28.0 3.80 5.26

(c) Specific electrical power energy consumption (SEPEC)

Run

No.

Drying

Temperature

(C)

Feed

rate

(ton/h)

Bed height

(m)

Min

(% dry-

basis)

SEPEC

(MJ/kg of water

evaporated)

Exp1 Sim2

1 130 3.12 0.115 25.9 0.90 0.82

2 130 4.82 0.115 26.8 0.77 0.73

3 140 4.72 0.147 26.7 0.73 0.60

4 140 4.82 0.115 24.1 0.66 0.54

5 150 6.42 0.119 25.9 0.70 0.416 150 6.09 0.150 25.9 0.85 0.61

7 150 5.10 0.150 26.1 0.79 0.61

8 150 4.82 0.115 28.0 0.48 0.46Note : 1Experimental results ; 2Simulated results (thin-layer equation developed using analytical

method)

18



DOI: 10.2202/1556-3758.1401


22/23

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11. Soponronnarit, S. and Prachayawarakorn, S., Optimum Strategy for Fluidized

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12. Soponronnarit, S., Prachayawarakorn, S. and Sripawatakul, O., Development

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13. Soponronnarit, S., Wetchama, S., Swasdisevi, T. and Poomsa-ad, N.,

Managing Moist Paddy by Drying, Tempering and Ambient Air Ventilation,International Journal of Drying Technology,17(1&2), 1999, 335-344.

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19


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DOI: 10.2202/1556-3758.1401
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drying strategies of fluidized bed dryer

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