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Solar Adsorption Cooling: A Case Study on the
Climatic Condition of Dhaka
Rifat. A. Rouf
School of Engineering and Computer Science, Independent University, Bangladesh, Dhaka, Bangladesh
Email: rifat_rouf@yahoo.com
K. C. A. Alam 1, Md. Abdul. H. Khan 2, Tasnuva Ashrafee 3and Mohammed Anwer 3
1 Department of Electronics and Communication Engineering, East-West University, Dhaka, Bangladesh
2 Department of Mathematics, Bangladesh University of Engineering and Technology, Dhaka, Bangladesh
3 School of Engineering and Computer Science, Independent University, Bangladesh, Dhaka, Bangladesh
Email: kcaalam@ewubd.edu
Abstract - An analytical investigation has been conducted on
the performance of an adsorption chiller driven by solar
collector panel for the climatic condition of Dhaka. A set of
mathematical model and simulation technique are exploited
to investigate the system performances of solar driven basic
adsorption chiller with silica gel-water as
adsorbent/adsorbate pair. For base run condition, at least
13 collectors (each of area 2.415 2
m) are essential to
achieve the required heat source temperature (around 85°
C) to provide 10 kW cooling capacity. It is seen that the
chiller provide 10kw cooling capacity at noon, while, the
system provides solar COP around 0.35. It is also observed
that the collector size can be reduced by optimizing cycle
time and chilled water outlet temperature can be controlled
by setting an appropriate chilled water flow rate.
Index Terms - Adsorption, solar heat, renewable energy, air-
conditioning, heat source temperature
I. INTRODUCTION
Global warming, change in the seasonal cycle,
limitation of primary energy compared to the need of the
growing global population, are the prime concern of the
twenty first century. Cooling and refrigeration are
essentials for modern day’s society to provide the human
comfort. Most of the technologies at present for
providing cooling or refrigeration are vapor compressor
technology. However, the vapor compressor refrigeration
device is one of the technologies responsible for ozone
layer destruction as most of these use HCFCs and HFCs.
Moreover, it also increases the dependency on the
primary energy resources. As a result, it is imperative to
reduce the primary energy consumption and to introduce
renewable energy for the sustainable development in the
global energy sector.
At present, absorption (liquid vapor absorption) is
most promising technology and is commercially available
alternative to vapor compressor refrigeration devices.
Although, solid vapor absorption technology termed as
adsorption technology have an additional advantage over
other systems, ability to be driven by heat source of
relatively low temperature heat source studied by
Kashiwagi “et al” [1], such that waste heat or solar heat.
For the last three decades investigations have been
carried out both mathematically and experimentally about
different features of adsorption technology.
It is well known that the performance of adsorption
cooling / heating system is lower than that of other heat
driven heating / cooling systems. Meunier [2] and Saha
“et al” [3] studied the advantage and development of
adsorption cycle. Many adsorbent/adsorbate pairs have
been investigated ([4], [5] and [6]) for adsorption
refrigeration/heat pump purposes. A very few of these
adsorbent/adsorbate pairs were found to be suitable to
utilize low grade waste heat (especially below 100 oC
temperature) as driving source. Silica gel-water pair is
well suited to this temperature range. Saha “et al.” [7],
Boelman “et al.” [8] and Chua “et al.” ([9] and [10])
studied adsorption refrigeration cycle using the silica gel-
water pair which can be driven by at least 80 oC heat
source with 30oC cooling source. To utilize even lower
temperature waste heat (around 50oC temperatures),
researchers investigated advanced adsorption
refrigeration cycles. Saha “et al.” [11] proposed and
analyzed a two stage and a three stage [12] adsorption
chiller. A parametric study on two stage cycle was carried
on by Alam “et al.” [13] in the same context. Hamamoto
“et al.” [14] studied two-stage cycle with different mass
ratio, while Alam “et al.” [15] and Khan “et al.” [16]
studied the reheat two stage cycle. Though the multistage
regeneration techniques enable the chiller to operate with
lower waste heat temperature, however, the performance
of these systems are very low.
The major intricacy for commercialization of
adsorption chiller is their bigger machine size and lower
performance. Motivated by this reason Pons and Poyelle
[17] proposed internal mass recovery cycle to achieve
relatively high cooling power utilizing lower heat source
temperature suitable to run a conventional two bed
adsorption refrigeration cycle. Alam “et al.” [18]
investigated a four bed mass recovery cycle utilizing the
pressure differences among the beds. Afterwards, Wang
[19] and Akahira “et al.” [20] showed that mass recovery
process in conventional two bed adsorption cycle
improves the cooling capacity significantly for the
relatively low regenerative temperature.
Using solar radiation, Sakoda and Suzuki [21] studied
the simultaneous transport of heat and adsorbate in closed
type adsorption cooling system. Li and Wang [22]
investigated the effect of collector parameters on the
performance of solar driven adsorption refrigeration
cycle. Yong and Sumathy [23] applied lumped parameter
model for solar driven two bed adsorption refrigeration
cycle. Clausse “et al.” [24] investigated the performances
of a small adsorption unit for residential air conditioning
in summer and heating during the winter period for the
climatic condition of Orly, France. Later, Zhang “et al.”
[25] studied solar powered adsorption cooling system.
Where, they investigated the operating characteristics of
silica gel-water pair as adsorbent/ adsorbate utilizing
lumped parameter model. Recently Alam “et al.” [26]
investigated the performances of solar collector driven
adsorption cooling system under the climatic condition of
Tokyo, Japan.
Since Bangladesh is a tropical country, solar panels
can be installed and used for day time cooling for the
office buildings, cold storages in the rural areas where we
can preserve food and medicine for emergency use. From
this context, a two bed adsorption cooling system which
is run by solar collector, with silica gel-water pair as
adsorbent/ adsorbate, is analyzed mathematically under
the climatic condition of Dhaka in the present study. The
place is located in the northern hemisphere at 6423 ′
oN
(latitude), and 3290 ′
oE (longitude). Investigation is done
on the collector size to get optimum performance. Also
the performance of the chiller had been studied for
different cycle time.
II. PRINCIPLE AND OPERATIONAL PROCESS OF THE
SYSTEM
A two- bed conventional adsorption cooling cycle
driven by solar heat has been considered. Silica gel-water
pair as adsorbent/ adsorbate has been chosen for the
present study. There are four thermodynamic steps in the
cycle, namely, (i) Pre-cooling (ii)
Adsorption/Evaporation (iii) Pre-heating and (iv)
Desorption/ Condensation process. No heat recovery or
mass recovery process is considered in the present study.
The adsorber(A1/A2) are alternately connected to the
solar collector to heat up the bed during preheating and
desorption/ condensation process and to the cooling
tower to cool down the bed during pre-cooling and
adsorption/ evaporation process. The heat transfer fluid
transport heat from the solar collector to the desorber and
returns the collector to regain heat from the collector. The
valve between adsorber and evaporator and the valve
between desorber and condenser are closed during pre-
cooling/ pre-heating period while, these are open during
adsorption/ evaporation and desorption/ condensation
1.
Figure1. Schematic of the solar driven adsorption space
cooling system.
process. The schematic of the adsorption cooling with
solar collector panel is presented in Fig. 1. The
characteristics of adsorbent/adsorbate (silica gel-water)
are utilized to produce useful cooling effect run by solar
powered adsorption chiller. The chilled water delivered
from the evaporator cools the floor of the house.
The operational process of two bed basic adsorption
cooling unit can be found in the literature Saha “et al.”
[7]. A detailed description of solar collector driven
adsorption cooling system is available in Alam “et al.”
[26].
A. Mathematical Model
During the adsorption step, the adsorber cooling
temperature is taken equal to the ambient temperature. It
is assumed that the temperature, pressure and
concentration throughout the adsorbent bed are uniform.
Based on these assumptions the energy balance equation
of the adsorbent bed is represented by
(){}
()
bedeva
bed
vsisi
bed
si
bedwsibedsisisipMM
TT
d
t
dq
CW
d
t
dq
WH
TCqWCWCW
dt
d
−⋅+⋅Δ
=++
,
,
δ
(
)
outbedinbedff TTCm ,, −
+
&,
(
)
(
)
ffbedbedinbedbedoutbed CmUATTTT &
/exp
,, −⋅
−
+
=
.
Where,
δ
equals to zero or one depending whether
adsorbent bed is working as desorber or adsorber.
The energy balance equation for the condenser is
represented by
(){}
()
bedcd
d
vrsi
d
si
cdrrcdMcdMcd
TT
dt
dq
CW
dt
dq
WL
TCWCW
dt
d
−+⋅−
=+
,
,,,
(
)
outcdincdfcdf TTCm ,,, −
+
&,
(
)
(
)
fcdfcdcdincdcdoutcd CmUATTTT ,,, /exp &
−⋅
−
+
=
.
The energy balance equation for the evaporator is
A1
A2
CPC
Solar
Col lecto r
Qsolar
Condenser
Evaporator
Cooling
tower
Chilled
water
(3)
(4)
(2)
(1)
(){}
()
cde
d
lrsi
a
si
emlreMeMe
TT
d
t
dq
CW
d
t
dq
WL
TCWCW
dt
d
−+⋅−
=+
,
,,,
(
)
,
,,, outchillinchillfchillf TTCm −+ &
(
)
(
)
./exp ,,, fchillfeeinchilleoutchill CmUATTTT &
−
⋅
−+=
The mass balance of the refrigerant inside the
evaporator is expressed as
.
,⎟
⎠
⎞
⎜
⎝
⎛+−= dt
dq
dt
dq
W
dt
dW da
si
re
The concentration in bed is
),( qqkasp
d
t
dq −= ∗
where, kasp=
()
)/(exp TRgasEaDs ⋅−⋅ ,
)/(.15 2
0RpDDs s
=,
() ()()
BB
TbPsTvPsAAq /⋅=
∗,
3
3
2
210 TATATAAAA +++= ,
3
3
2
210 TBTBTBBBB +++= .
The saturation pressure is calculated according to the
Antonie’s equation, as Saha “et al.” [7], where the values
of i
A’s and i
B’s will also be found. The energy balance
of each of the collector is calculated by the
manufacturers’ data.
The collector efficiency equation is considered to be
same as Clauss “et al.” [24].The cyclic average cooling
capacity (CACC) is calculated by the equation
()
./)( ,,, ∫−=
timeendofcycle
letimebeginofcyc cycleoutchillinchillfchillchill tdtTTCmCACC &
The cycle COP (coefficient of performance) and
solarCOP in a cycle ( sc
COP ) are calculated respectively by
the equations
()
()
,
,,
,,,
∫
∫
−
−
=timeendofcycle
letimebeginofcyc outdindff
timeendofcycle
letimebeginofcyc outchillinchillfchillchill
cycle dtTTCm
dtTTCm
COP
&
&
()
.
,,
∫
∫
⋅
−
=timeendofcycle
letimebeginofcyc cr
timeendofcycle
letimebeginofcyc outchillinchillchillchill
sc IdtAn
dtTTCm
COP
&
B. Simulation Procedure
Standard solar radiation data measured at horizontal
tilt have been supported by the Renewable Energy
Research Center (RERC), University of Dhaka (Latitude
23.46 N, Longitude 90.23 E). For the present study the
solar radiation data for the station of Dhaka has been
used. The monthly maximum and minimum average
temperature (°C) at Dhaka station is supported by
Bangladesh Meteorology Department (BMD).
Results are generated based on solar data of Dhaka in
April, chiller configuration are same as Saha “et al.” [7]
and collector data are same as Alam “et al.” [26]. In April
the sunrise time is at 5.5h and sun set at 18.5h, where as
maximum and minimum temperatures on that month are
34oC and 24oC respectively. The maximum solar
radiation in April is measured as 988 W/m 2. For
simulation the maximum measured radiation of the
month has been considered and sine function is used (as
Alam “et al.” [26]).
Implicit finite difference approximation method is
applied to solve the set of differential equations. The
water vapor concentration q in a bed is a nonlinear
function of pressure and temperature. It is almost
unfeasible to divide the concentration in terms of
temperature for the present time and previous time.
Hence, to begin with, the temperature for present step is
taken based on assumption. The pressure and
concentration are then calculated for the present step
based on this assumption of temperature. Later, gradually
the consequent steps are calculated based on the primary
concentration with the help of the finite difference
approximation. During this process, the newly calculated
temperature is checked with the assumed temperature. If
the difference is not less than convergence criteria, then a
new assumption is made. Once the convergence criteria
are fulfilled, the process goes for the next time step. The
tolerance for all the convergence criteria is 10 4−. The
initial temperature, pressure and concentration are set
based on the temperature of the beginning of the day.
Then the program runs for consecutive several days
unless the steady conditions arrive. That is, all the
conditions at the end of the day are similar to that of the
beginning of the previous day. In this paper all results are
presented for the 3rd day, since the system reached to its
steady state condition from day 3 i.e. all output appeared
to be identical for the consecutive days. The design and
the operating conditions used in the simulation are given
in Table I (attached in appendix).
Logical programming language FORTRAN with
Compaq visual Fortran compiler has been exploited to
obtain the numerical solution of the proposed model.
III. RESULT AND DISCUSSION
The comparison between measured and simulated
radiation data is presented in Fig. 2. The model for the
radiation shows good agreement with measured data for
April.
The temperature histories of collector outlet and bed,
for cycle time 800s and 1000s, are presented in Fig. 3 (a),
(b) and (c). The driving temperature level for the silica
gel-water pair is around 80°C (Saha “et al.” [7]). To
(8)
(7)
(6)
(10)
(11)
(9)
(5)
Figure 2. Measured and simulated radiation data
achieve the required temperature level with cycle time
800s, 16 collectors and with 1000s, 14 collectors are
used. The collector outlet temperature reaches 90°C
while the bed temperature is 85°C. However, it is also
observed that the same temperature level is achievable
when collector number is reduced to 13 with cycle time
1000s (Fig. 3 (c)).
However, increase in the cycle time for all the cases
increases the bed temperature which is not preferable for
the silica gel-water adsorption bed. On the other hand
decreasing in the cycle time causes decrease in driving
(a) 16 collector cycle time 800s (optimum cycle time)
(b) 14 collector cycle time 1000s (optimum cycle time)
(c) 13 collector cycle time 1000s (optimum cycle time)
Figure 3. Temperature profiles for collector and beds
source temperature.
Clearly there remain an optimum cycle time for
maximum cooling capacity (Saha “et al.” [7] and Chua
“et al.” [9]), the optimum cycle time for 16 collectors is
considered as 800s as driving heat source temperature is
achievable with this cycle time. In the same way, the
same optimum cycle times for both collector numbers 14
and 13 are considered as 1000s. It can be mentioned here
that the collector size can be reduced by taking longer
cycle time for solar heat driven adsorption cooling
system (Alam “et al” [26]). However, it may reduce
cooling capacity for taking excessive long cycle time.
Therefore, it is essential to take both driving source
temperature as well as cooling capacity into consideration
to select optimum cycle time. Clearly Fig. 4 (c) shows
that for optimum cycle time with 13 collectors the
cooling capacity is 10 kW at the middle of the day with
the base run condition.
(a) For 16 collectors cooling capacity (kW) for different cycle time
(b) For 14 collectors cooling capacity (kW) for different cycle time
(c) For 13 collectors cooling capacity (kW) for different cycle
time
Figure 4. Cooling capacity (kW) for different number of collectors
Conversely increase in the cycle time increases the
COP values of the system (Saha et al [7] and Chua “et al”
[9]). The maximum solar COP 0.35 and cycle COP 0.6 is
achievable by the proposed system when 1000s cycle
time is considered with 13 collectors (Fig. 5 (a) and (b)).
The increase of COP at afternoon happens due to the
inertia of collector materials (Fig. 5 (a)). At afternoon,
there is less heat input but there is relative higher cooling
production due to the inertia of materials of collector.
Therefore, there is slow increase of COP. However, it
starts declining suddenly when the radiation is too low to
heat up the heat transfer fluid. A sudden rise of cycle
COP is observed at late afternoon. This happens due to
the excessive long cycle time comparing with low
radiation at afternoon. Due to the long cycle time at
afternoon, there were some cooling production at the
beginning of that cycle but there is a very less heat input
in whole cycle time. If one takes variation in cycle time
for the different cycle in the whole day then this behavior
will not be observed for solar COP. Almost same
observation was found as for the cycle COP.
The chilled water outlet temperature histories have
been depicted in Fig. 6 for collector numbers 16, 14 and
13 with their respective optimum cycle time. The
temperature is shown during the pick hours of the day
time from 12.0h to 14.0h. The fluctuation of the chilled
water outlet temperature is 4°C. Chilled water outlet
temperature varies from 8oC to 12 oC, if 13 collectors
are used. However chilled water outlet temperature
decreases below 8°C when collector number increases.
In air conditioning system, CACC and COP are not
the only measurement of performances. If those values
(a) Solar COP in a cycle for different number of collectors
(b) Cycle COP for different number of collectors
Figure 5. Solar COP in a cycle and cycle COP for different number of
collectors
Figure 6. Chilled water outlet temperature histories
are higher but there is relatively higher temperature
chilled water outlet, then the system may not provide
comfortable temperature to the end user. For all the above
studies the volumetric flow rate of chilled water is
considered to be the same, which is 0.7kg/s. However,
the chilled water outlet temperature can be controlled by
adjusting the flow rate of chilled water.
Chilled water outlet temperature histories of 13
collectors with different volumetric flow rate have been
depicted in Fig. 7. Decreasing the volumetric flow of
chilled water to the evaporator results in decreasing the
temperature of chilled water outlet. The chilled water
outlet temperature goes down to 4.5°C when volumetric
flow is considered as 0.3kg/s and temperature varies from
4.5°C to 9.5°C. Therefore, it may be concluded that
chilled water outlet can be controlled by adjusting chilled
water flow rates.
On the other hand when volumetric flow rate
increases cooling capacity increases compared to the heat
input. These effects are depicted in Fig. 8 (a). The overall
cycle COP decreases when the volumetric flow
decreases. But at afternoon there is a sudden rise in the
cycle COP which is visible in Fig 8 (b). This effect is due
to the lower cooling capacity and comparative higher heat
input due to the inertia of the collector material.
Figure 7. Chilled water outlet temperature for 13 collectors different
chilled water flow rates
(a) CACC with different chilled water flow rates
(b) COP cycle with different chilled water flow rates
(c) COP sc with different chilled water flow rates
Figure 8. Performance of the chiller with 13 collectors cycle time
1000s with different chilled water flow rate
IV. CONCLUSION
A solar heat driven adsorption cooling system has
been analyzed mathematically based on the climatic
conditions of Dhaka, Bangladesh. A panel of CPC
(concentrated parbolic collector) has been used for the
present analysis. Each collector area approximates
2.415m². Based on the analysis the following conclusions
can be drawn.
• For the climatic condition of Dhaka 1000s cycle time
with 13 collectors is needed to raise the driving heat
source temperature to 85°C for the base run
condition.
• Cyclic average cooling capacity is around 10 kW at
12:00 noon for base run condition.
• Increase in the cycle time increases the COP of the
present system. The maximum cycle COP is 0.6 at
12:00 noon with base run condition.
• Maximum solar COP is around 0.35.
• The performance of the system increases with the
increase of the volumetric flow rate of chilled water.
• But the cooling effect to the end user can be
improved by adjusting the chilled water flow rate.
• The collector area can be reduced by proper selection
of cycle time.
APPENDIX A TABLE I
Design and the operating conditions used in the simulation
Symbol Description Value
bed
A Adsorbent bed heat transfer area 2
415.2 m
bed
U Heat transfer coefficient of bed KmW 2
/14.1724
tm
W Heat exchanger tube weight ( Cu ) kg2.51
fm
W Heat exchanger fin weight ( Al ) kg04.64
eva
A Evaporator heat transfer area 2
91.1 m
eva
U Evaporator heat transfer coefficient KmW 2
/54.2557
Meva
W, Evaporator heat exchanger tube weight
(Cu ) kg45.12
con
A Condenser heat transfer area 2
73.3 m
con
U Condenser heat transfer coefficient KmW 2
/23.4115
Mcon
W, Condenser heat exchanger tube weight
(Cu ) kg28.24
cr
A Each collector area 2
415.2 m
cp
W Weight of each pipe including absorber
sheet kg4913.0
p
N Number of pipe in each collector 9
hotf
m,
& Total mass flow rate to CPC panel or to
desorber skg /3.1
coolf
m,
& Cooling water flow rate to adsorber skg /3.1
si
W Weight of silica gel in each bed kg47
reva
W, Liquid refrigerant inside evaporator initially kg50
condf
m,
& Cold water flow rate to condenser skg /3.1
chillf
m,
& Chilled water flow rate skg /7.0
rcon
W, Condenser refrigerant inside condenser kg0.0
H
Δ
Heat of adsorption (silica gel bed) kgJE /0681.2
+
Rgas Water gas constant KkgJE ./0262.4
+
Ea Activation energy kgJE /0633.2
+
0s
D Diffusion coefficient smE /0454.2 2
−
Rp Particle diameter (Silica gel) mE 0335.0
−
cool
T Cooling source temperature C
o
30
inchill
T, Chilled water inlet temperature C
o
14
Ir
C,Specific heat of water (liquid phase) KkgJE ./0318.4
+
vr
C,Specific heat of water (vapor phase) KkgJE ./0389.1
+
cu
C Specific heat of copper ( Cu ) KkgJ ./386
al
C Specific heat of aluminum ( Al ) KkgJ ./905
si
C Specific heat of silica gel ( Si ) KkgJ ./924
L Latent heat of vaporization (water) kgJE /066.2
+
ACKNOWLEDGEMENT
The authors wish to thank Renewable energy research
centre, University of Dhaka and Bangladesh
Meteorological Department for their co-operation.
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Rifat Ara Rouf born in 1970 is currently
doing her Ph.D. in the field of solar heat
driven cooling and heating system in
Bangladesh University of Engineering
and Technology (BUET), Dhaka,
Bangladesh. She had completed her
Master of Philosophy in Applied
Mathematics from the same institute in
2007. Earlier she had completed her
masters in Applied Mathematics from University of Dhaka,
Bangladesh in 1996. Currently, she is working as a SENIOR
LECTURER in Independent University, Bangladesh (IUB since
January 2008.
Dr. K. C. Amanul Alam had completed
his Dr of Engineering in Mechanical
Engineering from Tokyo University of
Agriculture and Technology, Japan. He
had his Master of Philosophy and Master
of Science in Applied Mathematics from
University of Dhaka, Bangladesh. He
was also post doctoral fellow at CNAM,
Paris, France and JSPS post doctoral
fellow at Tokyo University of Agriculture and Technology,
Japan. .He started his academic career as a lecturer of
Mathematics at Bangladesh University of Engineering and
Technology. Currently, he is working as an Associate Professor
at East West University, Bangladesh. He has published many
articles in peer review international journals and attended many
international conferences. His research interest includes
mathematical investigation in thermal engineering specially
heat driven cooling system, Numerical approach in engineering
problems, Fluid mechanics, Energy systems.
Dr. Md. Abdul Hakim Khan had
completed his Ph. D. from University of
Bristol (U.K.) in 2001. He had his
Master of philosophy completed from
Bangladesh University of Engineering
and Technology, Bangladesh in 1998.
Earlier he had completed his Masters in
Applied Mathematics from the
University of Dhaka, Bangladesh.
Currently, He is Professor of Mathematics at Bangladesh
university of Engineering and Technology. Dr. Khan’s interest
is focused in the area of Singularity analysis on fluid motion by
summing power series applying Semi numerical methods:
Algebraic and Differential Approximants. His interest is also in
Extension, Analysis and improvement of some fluid dynamical
problem, such as, Kelvin-Helmholtz instability, Flow in a
Curved pipe etc.
Tasnuva Ashrafee had completed her
Master of Science (M.S.) in 2005,
Department of Applied Physics,
Electronics and Communication
Engineering, University of Dhaka,
Bangladesh. She has completed her
Bachelor of Science (B.Sc.) in 2004
from the same institution. She published
an article in the journal of Advanced
Materials Research. She is also a life member of Bangladesh
Association of Women Scientists.
Dr. Mohammed Anwer completed his
Ph. D. in Mechanical Engineering from
Arizona State University (USA) in 1989.
He also had his Master of Science from
the same university. His Bachelor degree
was completed from Bangladesh
University of Engineering and
Technology, Bangladesh in 1982.
Currently he is serving simultaneously as
the Dean and Professor of the school of engineering and
computer science at Independent University, Bangladesh (IUB).
He has published many articles in peer review international
journals and attended many international conferences. His
research interest includes Turbulence, Flow modeling,
Aerodynamics, Hydrodynamic stability, Experimental fluid
mechanics and Computational fluid mechanics.
