This document describes the design and fabrication of a low-cost fluidized bed reactor for drying grains. Key points:
1) The fluidized bed reactor was designed with a drying column, fluidized plate, inlet and outlet units, heating unit, and fan. It was tested for drying rice and wheat.
2) The reactor design calculations included determining the vessel volume and cross-sectional area, minimum and maximum fluidization velocities, inlet pipe flow rate, and mean residence time.
3) Fabrication of the reactor involved using mild steel for the structure and included a Hacco pipe, Brim plate, and valves. Performance testing showed drying times of 89% and 90% efficiency for rice and wheat
Experimental Analysis of Refrigeration system using Microchannel condenser & ...AM Publications
Micro channel condenser now days can be effectively used due to its compact size in automobile sector. For
its performance, refrigeration set up designed to detect experimental performance of microchannel condenser. In this
paper performance analysis of microchannel condenser compared with round tube and coil tube. In analysis of
microchannel condensers it can be found more effective at various loads and operating conditions. For review same size of
microchannel and round tube condenser are considered. From the previous experiments the micro-channel condenser was
made to have nearly an identical face area, depth and fin density as the round-tube condenser which was the baseline. Also
varying the refrigerants, C.O.P & Efficiency of micro channel the various reviews of reviewer micro channel condenser
can be efficient and also refrigerator system requires less power.
Experimental Analysis of Refrigeration system using Microchannel condenser & ...AM Publications
Micro channel condenser now days can be effectively used due to its compact size in automobile sector. For
its performance, refrigeration set up designed to detect experimental performance of microchannel condenser. In this
paper performance analysis of microchannel condenser compared with round tube and coil tube. In analysis of
microchannel condensers it can be found more effective at various loads and operating conditions. For review same size of
microchannel and round tube condenser are considered. From the previous experiments the micro-channel condenser was
made to have nearly an identical face area, depth and fin density as the round-tube condenser which was the baseline. Also
varying the refrigerants, C.O.P & Efficiency of micro channel the various reviews of reviewer micro channel condenser
can be efficient and also refrigerator system requires less power.
ABSTRACT
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
Post-combustion CO2 capture and its effects on power plantsHamid Abroshan
This slide is a presentation of a conference paper discussing the post-combustion Carbon Dioxide capture from steam power plants. The main question in this paper was to choose the best location in flue gas path, where flue gas will be extracted and sent to absorption tower.
International Journal of Computational Engineering Research(IJCER) is an intentional online Journal in English monthly publishing journal. This Journal publish original research work that contributes significantly to further the scientific knowledge in engineering and Technology.
this ppt contains all drying method of egg powder and starter culture powder. the problems exist in manufacturing of it and what are the recent advances in it.
ABSTRACT
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
Post-combustion CO2 capture and its effects on power plantsHamid Abroshan
This slide is a presentation of a conference paper discussing the post-combustion Carbon Dioxide capture from steam power plants. The main question in this paper was to choose the best location in flue gas path, where flue gas will be extracted and sent to absorption tower.
International Journal of Computational Engineering Research(IJCER) is an intentional online Journal in English monthly publishing journal. This Journal publish original research work that contributes significantly to further the scientific knowledge in engineering and Technology.
this ppt contains all drying method of egg powder and starter culture powder. the problems exist in manufacturing of it and what are the recent advances in it.
The processing technique employing a suspension or fluidization of small solid particles in a vertically rising stream of fluid usually gas so that fluid and solid come into intimate contact. This is a tool with many applications in the petroleum and chemical process industries. Suspensions of solid particles by vertically rising liquid streams are of lesser interest in modern processing, but have been shown to be of use, particularly in liquid contacting of ion-exchange resins. However, they come in this same classification and their use involves techniques of liquid settling, both free and hindered (sedimentation), classification, and density flotation.
Slides explaining the different methods of food preservation. Informative for students studying AS or A2 Food Technology. A summary of preservative methods and short exam questions at the end.
In many cases, the drying of mater
ials is the fina l operation i n manufac turing process
carried out immediately prior to pack ag ing and dispatch . Drying refer s to final
removal o f water, and the operation follow s e vapo ration , filtration or crystallization .
Effective Moisture Diffusivity and Activation Energy of Tomato in Thin Layer ...drboon
The aim of this paper is to report tomato slice moisture diffusivity data determined and activation energy from experimental drying kinetics. The thin-layer drying experiments were carried out under five air temperatures of 40, 50, 60, 70 and 80ºC, two air velocity 1.5, and 2 m/s and three level of relative humidity 20, 40 and 60%. It was observed that drying took place in the falling rate period. Moisture transfer from tomato slice was described by applying the Fick’s diffusion model. The effective diffusivity values changed from 9.9119×10^-10 to 6.4037×10^-9 m^2/s for the range of temperatures considered. An Arrhenius relation with an activation energy value of 33.3299 to 43.2287 kJ/mol and the diffusivity constant value of 1.7695×10^-4 to 3.09156×10^-2 m^2/s were obtained which shows the effect of drying air temperature, air velocity and relative humidity on the diffusivity.
International Journal of Engineering Research and Applications (IJERA) is an open access online peer reviewed international journal that publishes research and review articles in the fields of Computer Science, Neural Networks, Electrical Engineering, Software Engineering, Information Technology, Mechanical Engineering, Chemical Engineering, Plastic Engineering, Food Technology, Textile Engineering, Nano Technology & science, Power Electronics, Electronics & Communication Engineering, Computational mathematics, Image processing, Civil Engineering, Structural Engineering, Environmental Engineering, VLSI Testing & Low Power VLSI Design etc.
Theoretical Convective Heat Transfer Model Developement of Cold Storage Using...IJERA Editor
Energy crisis is one of the most important problems the world is facing now-a-days. With the increase of cost of electrical energy operating cost of cold storage storing is increasing which forces the increased cost price of the commodities that are kept. In this situation if the maximum heat energy(Q) is absorbed by the evaporator inside the cold room through convective heat transfer process in terms of –heat transfer due to convection and heat transfer due to condensation, more energy has to be wasted to maintain the evaporator space at the desired temperature range of 2- 8 degree centigrade. In this paper we have proposed a theoretical heat transfermodel of convective heat transfer incold storage using Taguchi L9 orthogonal array. Velocity of air(V), Temperature difference(dT), RelativeHumidity(RH)are the basic variable and three ranges are taken each of them in the model development. Graphical interpretations from the model justifies the reality
THERMODYNAMIC SIMULATION OF YEAR ROUND AIR CONDITIONING SYSTEM FOR VARIABLE R...IAEME Publication
This paper presents a study on different kinds of air conditioning systems in comparison to existing one to use through of the year. Mainly the system imparts all three regular weather conditions. Like hot and dry, hot and wet and cool and dry. For this the out let condition will be fix ed 25 °C dry bulb temperature (DBT) and 50% relative humidity. In the present paper, for maintaining room condition thermodynamic simulation is being done. For simulation we used excels solver software. If atmospheric condition like relative humidity of air is changed, the year round air conditioning equipments change own parameters such as volume of cellulose cooling pad of evaporating cooler, temperature of cooling coil in hot and dry as well as hot and wet weather conditions, temperature of preheat and reheat coil in cold and dry weather to maintain the room condition.
NUMERICAL INVESTIGATION OF NATURAL CONVECTION HEAT TRANSFER FROM CIRCULAR CYL...IAEME Publication
In the present work, the enhancement of natural convection heat transfer utilizing nanofluids as working fluid from horizontal circular cylinder situated in a square enclosure is investigated numerically. The type of the nanofluid is the water-based copper Cu. A model is developed to analyze heat transfer performance of nanofluids inside an enclosure taking into account the solid particle dispersionrs on the flow and heat transfer characteristics. The study uses different Raylieh
numbers (104 , 105 , and 106 ), different enclosure width to cylinder diameter ratios W/D (1.667, 2.5 and 5) and volume fraction of nanoparticles between 0 to 0.2. The work included the solution of the governing equations in the vorticity-stream function formulation which were transformed into body fitted coordinate system
Optimization of “T”-Shaped Fins Geometry Using Constructal Theory and “FEA” C...IJERA Editor
This paper reports the geometric (constructal) optimization of T-shaped fin assemblies, where the objective is to maximize the global thermal conductance of the assembly, subject to total volume and fin-material constraints. Assemblies of plate fins are considered. It is shown that every geometric feature of the assembly is delivered by the optimization principle and the constraints. These optimal features are reported in dimensionless terms for this entire class of fin assemblies. Based on the constructal theory by Dr. A Bejan, T-shaped fins are developed for better heat conductance as compared to conventional fins. Now the geometry of this T type of fin contains many geometry parameters which affect the overall conductance of the fin. With the same material constraint and volume constraints optimal geometry ratios has been calculated so as to design the fin for its best performance. With focus to the practical situations and heat flow patterns, it is quite complex to calculate the temperatures on a T-shaped fin. It requires the help of FEA concepts and CAE software to optimize the geometry.
Optimization of Air Preheater for compactness of shell by evaluating performa...Nemish Kanwar
Designing of an Air Preheater with increased performance from an existing design through alteration in baffle placement. Analysis of 4 Baffle designs for segmented Baffle case was done using Ansys Fluent. The net heat recovery rate was computed by subtracting pump work from heat recovered. Based on the result, Air Preheater design was recommended.
Numerical Simulation of Solar Greenhouse Dryer Using Computational Fluid Dyna...RSIS International
Moisture removal from crops and other food items is
one of the ways to preserve them for longer duration. Previously,
drying openly in sun was used to reduce moisture content. But it
had some disadvantages like contamination due to dirt and other
unwanted elements as well as attack by rodents and birds.
Drying in covered close space with vents would be helpful in
overcoming these problems. Solar greenhouse dryers are the
close conduits in which crops can be dried without negatively
affecting the nutrition value. The factors affecting the crop
drying are solar radiation, climatic conditions, material of which
the dryer is made of and shape of the dryer. A lot of
experimental investigations have been done to improve the
drying rate. With the advances in computational power and
numerical techniques, Computational Fluid Dynamics (CFD) has
emerged as a powerful tool to optimize any design. In the present
study, simulations have been done on greenhouse dryer with
modifications to identify the temperature distribution with
variation in wind velocity. Different radiation levels have also
been found out at different locations in the dryer. The model of
the dryer has been created in CREO 5.0 and analysis has been
performed using ANSYS 14.0. The simulation has been done for
both forced and natural convection. Obtained results have been
validated with the experimental work done by previous works.
Better drying rate has been obtained for forced circulation as
compared to natural convection which is in agreement with the
available experimental results.
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Design and fabrication of a low cost fluidized
1. Innovative Systems Design and Engineering www.iiste.org
ISSN 2222-1727 (Paper) ISSN 2222-2871 (Online)
Vol 3, No 3, 2012
Design and Fabrication of a Low Cost Fluidized
Bed Reactor
Oluleye, A. E. and Ogungbemi, A .A. and Anyaeche*, C.O.
Department of Industrial and Production Engineering University of Ibadan, Ibadan, Nigeria.
*E-mail of the corresponding author: osita.anyaeche@mail.ui.edu.ng and 3osyanya@yahoo.com.
Abstract
Many farmers now use the dryer as a part of their normal grain-harvesting system even during wet seasons.
This helps in reducing spoilage. However, most available dryers are expensive to purchase and maintain.
This work therefore is an attempt to develop a simple low cost drying bed that can lead to reduced drying
time. The fluidized bed designed and fabricated in this work consists of the drying column, fluidized plate,
the inlet and outlet unit, the heating unit and the fan. The evaluation considered the drying time and
temperature in achieving quality. The drying efficiency and the amount of moisture reduced per time and
were investigated using rice and wheat with moisture contents of 23% and 33% respectively. The dryer has
shorter drying times and efficiencies of 89% and 90% for rice and wheat respectively.
Keywords: Fluidized Bed, Grain Drying, Low Cost Design.
1. Introduction
Grain drying is now common in many countries. Instead of drying only during very wet harvest seasons,
many farmers now use a dryer as a part of their normal grain-harvesting system. This helps in eliminating
spoilage in storage and improvement on early harvesting. The fluidized beds have been developed for
different physical and chemical operations, such as transportation systems and chemical reaction processes
(Baeyens and Geldart, 1986; Kunii and Levenspiel, 1991).Studies (Baeyens and Geldart, 1986; Kunii and
Levenspiel, 1991) however show that the traditional and some commercial grain dryers consume
considerable time and energy in their operations and available dryers are very expensive. Therefore, there is
the need to develop dryers that would lead to time reduction of grain without compromising efficiency and
also give reduced operating cost (Kunii and Levenspiel, 1991).
In this work an attempt is made to design and construct a low cost fluidized bed reactor that will be used in
the drying of food products and its performance was also evaluated.
2. Overview
The drying process is an operation that aims at a reduction of the moisture content in most products,
industrialized or not, to guarantee their preservation in storage and transport (Keey, 1992). The process of
fluidization with hot air is highly attractive for the drying of powders and wet granular materials. This
technique has been used industrially and is currently quite common in the drying of coarse materials,
pharmaceuticals and food products among other solids in different countries of the world (Aberuagba et al,
2005). The major parts of the fluidized bed reactors are: the fluidization vessel, the solids discharge, dust
separator for the exit gas, the air supply and heat supply.
A fluidized bed is a vessel containing a bed of solid particles, e.g. sand or catalytically active particles, and
a method of introducing gas from below. It is a machine in which a continuous flow of wet granular
material is dried. In this process the air velocity of the drying air is adjusted in such a way that the layer of
product is maintained in a fluidized state (Sripawatakul, 1994).
24
2. Innovative Systems Design and Engineering www.iiste.org
ISSN 2222-1727 (Paper) ISSN 2222-2871 (Online)
Vol 3, No 3, 2012
Uniform processing conditions are achieved by passing a gas (usually air) through a product layer under
controlled velocity conditions to create a fluidized state. Heat may be effectively introduced by heating
surfaces (panels or tubes) immersed in the fluidized layer (Queiroz et al, 2005).
2.1.Some Advantages of Fluidized Bed Reactor
One advantage of using fluidized bed reactor as a dryer is the close control of conditions so that
predetermined amount of free moisture may be left with the solids and to prevent dusting of the product
during subsequent material handling operations (Perry and Green, 1998). Other advantages include:
• Uniform temperature throughout the material bed by enhanced heat transfer
• Improved gas-solid contact, which results in faster rate of reaction
• Uniform product quality from extensive bed mixing and controlled reaction conditions
Fluidized bed technology has been successfully applied to the synthesis of materials via gas-solid or solid-
solid reactions, coating via chemical vapor deposition, calcinations, sintering, thermal decomposition,
thermal treatment, and drying (Harper, 2005).
The disadvantages of fluidized beds are summarized below:
• Bubbling beds of fine particles are difficult to predict and are less efficient,
• Rapid mixing of solids causes non-uniform residence times for continuous flow reactors,
• Particle comminuting (breakup) is common,
• Pipe and vessel walls erode due to collisions by particles.
Figure 1: A typical fluidized bed reactor
Other factors that also affect the performance include: Bed temperature, particle size, fluidization velocity,
bed height, tube location, heat transfer coefficient and pressure drop.
2.2 Design Parameters
A full listing of the terms and notations is presented in appendix 1. The design calculations for this work
are based on the works of Levenspiel (1991), Sripawatakul (1994) and Soponronnarit (1999). Also the use
of the conventional formula for the calculation of the volume (V) and cross sectional area (Ac) of a
cylinder was adopted.. These and other relevant formulae are summarized below:
V = π r 2 h Volume of the reactor 1
Ac = πD2 /4 = Cross sectional area (Ac) 2
25
3. Innovative Systems Design and Engineering www.iiste.org
ISSN 2222-1727 (Paper) ISSN 2222-2871 (Online)
Vol 3, No 3, 2012
The net gravitational force (∆p) needed in the fluidized vessel that would be exerted on the particles inside
the vessel.
∆p = g ( ρc − ρ g ) (1 − ε ) h 3
The emf is the void fraction at the point of the minimum fluidization. It appears in many of the equations
describing the fluid-bed characteristics.
0.029 0.021
µ2 ρg
emf = 0.586 (ψ )
−0.072
3 4
ρ gη dp ρc
Reynolds number (Re): This is a dimensionless parameter that affects the characteristics of the two
velocities involved in the study i.e. the minimum and the maximum fluidization velocity. This is expressed
124dpVp
as: Re = 5
µ
Minimum fluidization velocity (umf): This is the velocity required to begin the fluidization at which the
weight of particles’ gravitational force equals the drag on the particles from the rising gas.
(ψ dp ) η
2
emf 3
umf = , where ⋅η = g ( ρ c − ρ g ) 6
150 µ 1 − emf
Maximum fluidization velocity (Ut): The maximum fluidization velocity was calculated for the reactor so
as to avoid chaotic situation where the particles will not be blown out of the reactor.
η dp 2 1.78 ×10−2η 2 1
Ut = = [ ]3 dp 8
18µ ρ gµ
Inlet pipe flow ( f r ): The expression adopted based on Eefisso for calculating different flow rates in a
system (www.eefisso.com, 2007).
1
f r = π Pi 2V 9
4
Mean residence time (τ): This is the mean time during with which the molecules remain on the surface of
the bed .i.e. the mean time interval between impact and drying (IUPAC Compendium of Chemical
Terminology, 1997 ; Sriparratakul, 1994).
V
τ= 10.
f
3. Methodology
In this section we give the major components, the design calculations and the fabrication of the fluidized
bed.
3.1 Design Calculations
In this section we present the design parameters of the components of the bed, the design computations and
performance tests carried out on the reactor.
3.1.1 The fluidizing vessel Requirements
The fluidization vessel was designed to have a volume of 100cm3 so as to have a maximum bed height of
200mm (20cm). The height and the diameter chosen for this design were based on the fact that it was being
designed on a small scale which will still bring appreciable outputs, and not to occupy much space when
fully installed.
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For the volume of the fluidizing chamber the use of the conventional formula V = π r 2 h for volume
determination was adopted.
V = πr2h =3.142x242 x 56 m3
3.1.2 Cross sectional Area of the reactor (Ac)
The cross sectional area of the empty vessel.
Ac = πD 2r/4 = (3.142 x 48 2) /4 = 1809.79 cm2
3.1.3 Net Gravitational force
The net gravitational force needed in the fluidized vessel bed reactor (dryer that would be exerted on the
particles inside the vessel (Saponronnarit, 1999).
∆p = g(ρc - ρg)(1 - ε) h = 9.81(1.3 – 0.00107)(1. 0.84)24
= 4.89N/m2
3.1.4 emf for the reactor
The emf for the reactor needed in determining the minimum fluidization velocity for the reactor. This emf
is the void fraction at the point of the minimum fluidization. It appears in many of the equations describing
the fluid-bed characteristics (Saponronnarit, 1999).
is computed thus:
Emf = 0.586(Ψ)-0.072 (µ2/ρgηdp3) 0.029 (ρg/ρc ) 0.021
= 0.586(0.7)-0.072 ({1.5x10-4}2/(0.00107x12.7295x0.0053) 0.029 (0.0017/ 1.3) 0.021
= 0.7202
Ψ is the measure of particles not ideal in both shape and roughness (Wei and Yu, 1994). It is calculated by
visualizing a sphere whose volume is equal to the particles and dividing the surface area of the sphere by the
measured surface area of the particle.
3.1.5 Reynolds number
This is a dimensionless parameter that affects the characteristics of the two velocities involved in the study
i.e. the minimum and the maximum fluidization velocity.
Re = (124dpVp)/ µ = (124 x 0.05 x 6.5458 x10 -5) / (1.5x10-4)
= 2.7
Since the Re is less than 10, it gives the type of flow in the fluidizing vessel as a laminar flow and the type
of maximum fluidizing velocity needed for the system.
3.1.6 Minimum fluidization velocity (umf).
Minimum fluidization velocity: This is the minimum velocity needed to blow the particles of the bed. It is
the velocity required to begin the fluidization at which the weight of particles gravitational force equals the
drag on the particles from the rising gas.
Umf =[(Ψdp) 2 / (150µ)] η [(emf) 3/(1-emf)], where η = g(ρc- ρg) = 12.7295
=[(0.7x 0.05) 2 / (150 x 1.5x10-4)] 12.7295 [(0.47) 3/(1-0.47)]
= 0.1357m/s
3.1.7 Maximum fluidization velocity.
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The maximum velocity needed for the particles inside the reactor. The maximum fluidization velocity was
calculated for the reactor so as to avoid chaotic situation where the particles will not be blown out of the
reactor. The drag on the particles will surpass the gravitational force on the particle and the particles will be
entrained in the gas.
Since the Re number is less than 10, we use the equation, ut = (ηdp2)/[18µ]
Thus ut = (ηdp2)/ 18µ = 12.795 x 0.052/(18 x 1.5 x 10-4)
= 11.78m/s
3.1.8 The inlet pipe
The feed inlet pipe was designed to supply feed at a rate of 1.988m3/min, so as not to create a turbulent
situation or flooding of the reactor. The pipe was attached to the reactor at an angle of 30 degrees. The
expression used in the calculation of the pipe flow rate into the vessel was based on the work of Eefisso for
calculating different flow rates (www.eefisso.com, 2007).
This is given as: f r = 1 π Pi 2V = [3.142 x (1.049)2 x 2.3] /4
4
= 1.988m3/s
3.1.9 Mean residence time for the chamber.
This is the mean time during with which the molecules remain on the surface of the bed .i.e. the mean time
interval between impact and drying (IUPAC Compendium of Chemical Terminology, 1997; Sriparratakul,
1994).
τ = v/f = 101.248/1.988
= 50.9799s
3.1.10 Pressure drop in the equipment
∆P, the pressure drop across the bed is closely related to drag force,
The pressure drop was calculated based on the work of Jayasuriya and Manrique (2005).
∆Pg = hA∆t
= h x 0.00165x (413 - 353)
= 0.099h N/m2
3.1.11 Elutriation of Particles from fluidized bed reactor
The elutriation process causes a decrease in the particle concentration in the column and the concentration
may be empirically modeled by an Arrhenius type expression
C = Co e− Mt ; where C = concentration at time t Co = the initial concentration M = empirical constant.
3.1.12 Power Requirement.
The power required for setting the designed fluidized bed into operation and the continuation of the
operation was based on the suggestions of (Shott et al., 1975). They suggested horse power requirements
for different types of flow actions and different reactions.
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TABLE 1: Suggested Horse Power Requirements (hp/1000gal).
Type of flow Power requirement Types of operations
Mild 0.5 – 2 Mixing, blending
Medium 2–5 Heat transfer, suspension, gas absorption
Violent 5 – 10 Reactions, Emulsification,
3.2 Bill of Quantities
The quantities and price of material need for the work are summarized in Table 2.
Table 2: Bill of Quantities
(a) Construction cost
s/n Materials Specifications Quantity Rate (Naira) Cost (Naira)
1 Mild steel G18 1.2×1.2 m 4 4000 16000
2 Mild steel G16 1.2×1.2 m 2 3750 7000
3 Hacco pipe 100×4 m 1 5000 5000
4 Brim plate 4×4 m 1 2000 2000
5 Valves 2 600 1200
6 Electrode 2 1200 2400
7 Electric motor 1 8000 8000
8 Bolts and nuts 20 30 600
9 Electrode 100 10 1000
10 Paints 1 1850 1850
11 Miscellaneous 5000
Total 50,550.00
Adding 10% contingency to the total cost give the total design cost to be 55605 Naira.
Adding 25% margin to the total design cost, the machine can be sold at a price of 69509.25 Naira which is
still cheaper when compared to other commercial dryers of 126,556. Naira.
3.3 Fabrication of the Fluidize Bed
The fabrication of the Fluidize Bed was carried out using the data from the above computations. In addition
to that, the following precaution are taken into consideration.
a. The fluidization vessel: the vessel was designed to have the capacity of receiving heated fluid (hot
air) from the heat source and to house the porous disk.
b. The solid inlet feeders:
c. Solids discharge
d. Dust separator for the exit gas: The dust collector is usually designed to trap any solid, which
might want to escape with the exit gas.
e. The air supply: the use of an electric motor fan was used to supply air to the system.
f. Heat supply: the heat was supplied by a heating element at a temperature of 1150 Celsius.
3.4 Performance Tests
Tests were carried out on the designed machine to ascertain its performance. The analysis was carried out
on the fluidization reactor to determine the moisture reduction of rice and wheat during the drying process.
Before the fluidization process, the weights of the rice and wheat were measured. The grains were fed
manually into the equipment and the outputs from the grains outlet were subsequently collected and
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weighed. The temperature and pressure were kept constant at the heating chamber throughout the whole
process and the time was varied between ten and thirty minutes for different quantities of food samples.
The temperature inside the chamber was found to be 63 degrees centigrade.
The aim of the experiment was to monitor the reduction of moisture in food grains at different time
intervals and constant temperature using rice and wheat as the samples.
For the evaluation process the following parameters were employed based on the work of Okoli (1991) and
Ojediran and Jekayinfa (2002).
Sample evaluations were done using the following as the guide.
Moisture content in sample (mc) = original weight (Os) less final weight (Fs).
i.e. mc = Os – Fs 12
Drying time for samples
(τ) = (.x1 − xr) / N 13
% moisture content (Mc)
Loss in weight × 100
Weight of the original sample
mc
Mc = × 100 14
Os
Efficiency of the system (Eff):
1 –Mc = Eff 15
The results of the tests on the designed fluidized bed reactor were taken at 5 minutes interval to ascertain its
efficiency; and also were compared with those of some commercial dryers. The results and the graphs are
the discussions are presented in section 4.
4.0 Results and Discussion
4.1 Results of Performance Evaluation
Table 3: Percentage Moisture Reduction in Grain Samples
Time (minutes) Rice (% moisture content reduced) Wheat (% moisture content reduced)
10 4.774 3.212
15 4.896 5.576
20 5.682 7.114
25 7.550 8.605
30 8.048 9.420
35 11.178 9.670
For the results of efficiency of the designed equipment are presented in table 4.
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Table 4: Efficiencies of the Fluid Bed Dryer
Time (minutes) Rice efficiency Wheat efficiency
10 0.95 0.97
15 0.95 0.94
20 0.94 0.93
25 0.92 0.91
30 0.92 0.91
35 0.89 0.90
Table 5: Performance Test Results Of Commercial Dryers At 20 Minutes
Drying air Inlet moisture of Outlet moisture of Moisture reduction in grain
temperature (oC) grain (%) grain (%) (%)
115 22.0 20.1 1.9
115 26.0 22.5 3.5
115 28.7 22.5 6.2
115 30.6 23.0 7.6
115 27.0 21.0 6.0
Source: Soponronnarit (1999).
R ic e
2 6 W h e a t
R ic e
W h e a t
weight of samples
0 .9 8
0 .9 7
0 .9 6
0 .9 5
2 4
% moisture content
0 .9 4
0 .9 3
0 .9 2
0 .9 1
8 1 0 1 2 1 4 1 6 1 8 2 0 2 2 2 4 2 6 2 8 3 0 3 2 3 4 3 6
0 .9 0 tim e ( m in u te s )
0 .8 9
Figure 2: Weight 8of samples 2 1 4 time.
1 0 1
against 1 6 1 8 2 0 2 2 2 4 2 6 2 8 3 0 3 2 3 4 3 6
tim e ( m in u te s )
An examination of figure 2 shows that as the time in increased the moisture content in particles and their
corresponding weights decreases because the moisture content contributed to the total weight of the
particles. This shows that the fluidized bed dyer is a good medium for drying of rice and wheat.
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R ic e
36
34
32
30
28
drying time (minutes)
26
24
22
20
18
16
14
12
10
8
4 6 8 10 12
m o is t u r e c o n t e n t r e d u c e d
F ig u r e 4 . 3 G r a p h o f d r y in g t im e a g a in s t t h e p e r c e n t a g e m o is t u r e c o n t e n t r e d u c e d in r ic e
Fig 3: Drying time against Percentage moisture content in rice.
W heat
36
34
32
30
28
drying time (minutes)
26
24
22
20
18
16
14
12
10
8
4 6 8 10 12
m o is tu r e c o n te n t r e d u c e d
F ig u r e 4 . 4 G r a p h o f d r y i n g t im e a g a in s t t h e p e r c e n t a g e m o is t u r e c o n t e n t r e d u c e d in w h e a t
Fig 4: Drying time verses %age moisture in wheat
Figures 3 and 4 show the conformity of the fluidized bed dryer to the different drying principles in the
literature. As the time is increased so also the moisture reduced until it gets to the equilibrium stage where
no moisture will be removed from the grains. Wheat shows a better curve than rice since they are smaller in
size and weight than rice. This is probably because the smaller seeds or grains have higher resistance to
airflow and therefore reducing the action on fan outputs.
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B
8
% moisture reduced
6
4
2
110 115 120 125 130 135 140 145 150 155
temperature degree
Figure 4.5 graph of%moisture reduced in commercial fluidized bed dryer against temperature at 20minutes
Fig 5: Percentage of moisture Commercial fluidized bed against Temperature (20 min)
Figure 5 shows the amount of moisture reduced at different temperatures at the time of 20 minutes.
Comparing the efficiencies at the temperature of 115 degrees centigrade and at 20 minutes with the
designed fluidized bed dryer, it was seen that the efficiencies is lower when compared with the designed
dryer.
5.1 Conclusions
In this work the design and fabrication procedure for a low cost fluidized bed has been demonstrated. From
the results obtained, it can be inferred that the weights of different samples affect the fluidization process,
because grains with higher weights show less resistance to air flow in the system.
In addition to that, increasing the airflow speed increases the drying rate but also increases the power
consumption in the system, smaller grains show high resistance to airflow therefore reducing the fan
outputs and also increasing the amount of moisture reduced in the grains by the hot air giving higher power
efficiency in wheat than in rice.
A fluidized bed dryer can be competitive with other convectional drying methods especially at high
moisture level and low energy consumption. Drying on fluidized bed is a reliable and economical method
for drying of light weighted grains.
Further work may investigate the energy consumption. Further research should be carried out on other food
grains that have different weights and moisture content than the rice and wheat used in this study.
References:
Baeyens, J. and Geldart, D., Gas Fluidization Technology, Wiley, London, chapter Solids
mixing, p 79–86 (1986).
Kunii, D., and Levenspiel, O., (1991), Fluidization Engineering 2nd edition. Butterworth-Heinemann
Corporation.
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Vol 3, No 3, 2012
Keey, R. B., (1992) Drying of Loose and Particulate Materials, New York: Hemishere Publishers, p 29-32.
Aberuagba. F, Odigure. J. O, Adeboye .K. R, and Olutoye. M. A, (2005), Fluidization Characteristics of a
Prototype Fluidized Bed Reactor, Leonardo Journal of Sciences.
Sripawatakul, O.,(1994), Study of drying Paddy by Cross-Flow Fluidization Technique, Master thesis,
Faculty of Engineering, King Mongkutis Institute of Technology, Thonburi, Bangkok, Thailand.
Queiroz, C.A.R., Carvalho, R.J, and Moura, F. J. (2005), Oxidation of zinc sulphide concentrate in a
fluidized bed reactor-part 1: characterization of the fluid dynamics of the particle bed”, Brazilian journal of
chemical engineering, vol 22, number 01, p 117-125 (Jan-March, 2005).
Soponronnarit, S. , (1999), Fluidized-Bed paddy Drying, Science Asia Journal 25, p 51-56.
Eefisso company, www.eefisso.com, (April, 2007).
IUPAC Compendium of Chemical Terminology, (1997).
Wen, C.Y., and Yu,Y.H.,(1994), AIChE J., 12, 610. (1994).
Jayasuriya. J and Marique. A, (2005), laboratory notes on heat transfer measurement in fluidized bed
combustion reactor, Stockholm, (3- Feb-2005).
Shott, N.R, Weinstein, B and LaBombard, D., (1975), Motionless Mixers in Plastic Processing, Chem Eng.
Prog, Vol 71, No 1.
Okoli, J.U. (1991), Some Factors Affecting the Efficiency of Locally Fabricated Palm Kennel/Shell Nut
Crackers, NIIE Annual Conference, Ibadan.
Ojediran, J.O and Jekayinfa. S.O, (2002), Performance Evaluation of a Centrifugal Palm Nut Cracker,
Journal of Applied Science and Technology, Ibadan.
NOTATIONS
Here we define the notations used in this work.
τ = drying time (seconds)
X1= initial moisture (kgh20kg-1.d.m)
xr = relative moisture (kgh20kg-1.d.m)
N = drying velocity (kgh20kg-1.d.m)
υ = velocity (ms-1)
υ1 = minimal fluidization speed (ms-1)
m.d.m = dry matter, mass (kg)
β = dimensionless coefficient
ρ = density (kg-3)
ρ1 = bulk density (kg-3)
Wost = water content in fresh material. (Kg/kg)
A = heating element area
D= Reactor diameter
H= Reactor height
P= Pressure
V= Air velocity
ε = porosity
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g = Acceleration due to gravity
π = pi
ρg = 1.07× 10-3g/cm3
ψ = 0.7
µ = 1.5×10-4 poise
h = Bed height
Vp = Particle diameter
Pi = Pipe Diameter
Umf = minimum fluidization velocity
Ut = maximum fluidization velocity
Mc = % moisture content
Mc = moisture content
Ac = cross sectional area
V = volume
Plate 1: Constructed fluidized bed dryer.
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