DOI : 10.17577/IJERTV13IS070018
- Open Access
- Authors : Kingsley C. Egemba, Temitope K. Awodeyi
- Paper ID : IJERTV13IS070018
- Volume & Issue : Volume 13, Issue 07 (July 2024)
- Published (First Online): 19-07-2024
- ISSN (Online) : 2278-0181
- Publisher Name : IJERT
- License:
This work is licensed under a Creative Commons Attribution 4.0 International License
Title of Paper: Production of Biodiesel From Rubber Seed Oil using K-Pumice Catalyst: Modeling and Kinetics
AUTHORS:
Kingsley C. EGEMBA, Temitope K. AWODEYI
Department of Chemical Engineering, University of Uyo, Uyo, Nigeria.
ABSTRACT
A
The production of biodiesel from rubber seed oil using a synthesized composite catalyst (K-Pumice) was investigated. A two-step approach involving an acid catalyst treatment, followed by an alkali catalyzed transesterification, was used to convert the oil into fatty acid methyl ester (FAME). In the first step, extracted rubber seed oil was pretreated with methanol and sulphuric acid to reduce its acid value. Reaction time (90 to 180 minutes), temperature (40 to 60OC), catalyst amount (2 to 10 wt.% of oil) and methanol to oil ratio (6:1 to 10:1 vol/vol) were the transesterification process variables varied to study their effects on biodiesel yield. A fit of the developed quadratic models predicted biodiesel yield to the actual biodiesel yield data, gave an R2-value of 0.9978 and an F-value of 475.5. The high R2-value and F-value are indicative of a well fitted and reliable model. All the variables had positive effects on biodiesel yield. However, beyond the optimum values of 150 minutes, 55oC, 8 wt.% of oil and 9:1 vol/vol for time, temperature, catalyst amount and methanol to oil ratio respectively, the biodiesel yield was observed to decrease. The optimum yield of biodiesel was found to be 75.97%. The second- order kinetic model suitably described the biodiesel production process, with a rate expression of -rA = 0.0221 C 2 at 55OC, and an activation energy of 30.030KJmol-1. The produced biodiesel had a specific gravity of 0.87; an acid value of 0.43(mgKOH); flash point of 150OC and kinematic viscosity of 5.0 (mm2/s) at 40OC. The values of these properties were within ASTM D6751 standards, and compared favourably with values reported by other studies.
KEYWORDS: Biodiesel production, Rubber seed oil, K-Pumice, Modeling, Optimization, Kinetics
-
INTRODUCTION
There is a steady increase in the global energy demand [1]. Environmental concerns and sustainability issues have led to biodiesel being identified as a viable alternative to the traditional fossil fuels [2]. Biodiesel has over the years gained significant attention as it is renewable, non-toxic, biodegradable, less pollutant emitting, and a more environmentally friendly fuel source than fossil diesel fuel currently available. It has been studied as one possible solution in the imminent depletion of fossil fuels and is widely regarded
to be very sustainable and eco-friendly [3]. Biodiesel is produced by transesterification of oils or fats derived from plant matter or animal wastes. The feedstock used to produce biodiesel makes use of CO2 in the atmosphere in its photosynthesis [4]. During combustion, biodiesel does not emit sulfur or aromatic based compounds and it has a lower hydrocarbon and particulate matter emission. In total, biodiesel has 41% lesser greenhouse gas emission when compared to diesel [5]. Feedstock accounts for 60 75% of the total biodiesel production costs; and biodiesel production from cheap low-cost materials will reduce its cost, thus making it more competitive than conventional fossil fuels [1]. The oils that can be used as feedstock for biodiesel production can be grouped as edible oils, non-edible oils and waste oils. Most of the biodiesel production feedstock used of recent is from edible oil plants such as palm oil, rapeseed, sunflower and soybean. These compete with food, cosmetic and pharmaceutical uses, leading to food-fuel crisis and high price of biodiesel generated thereof [1]. In order to minimize food security concerns and biodiesel production costs, current research focuses on the use of non- edible oils and waste oils [6]. Rubber tree (Hevea brasiliensis) is one of the few versatile bioenergy crops with non-edible oil that could be exploited as low-cost industrial oil for the production of biodiesel.
The basic reaction involved in biodiesel production has been reviewed in literature. This is the reaction between triglycerides and methanol in the presence of a catalyst (transesterification), yielding the desired Fatty Acid Methyl Ester (FAME) and a byproduct, glycerol [7]. Because of the high free fatty acid content of rubber seed oil, and the need to avoid soap formation, conversion to biodiesel follows a two-step process involving a free fatty acid reduction step (acid esterification step) and the biodiesel production step (alkaline transesterification step). The current work focuses on the modeling, optimization and kinetics of the conversion of rubber seed oil to biodiesel using K- Pumice as an alkaline catalyst.
-
MATERIALS AND METHODS
The rubber seeds were milled and dried to constant weight in an oven (DHG-9101 Laboratory dry oven) at 105OC to constant weight. The seed oil was then extracted using n-hexane. K- Pumice was prepared using the method described in [4]. For the acid catalyzed esterification of the rubber seed oil, H2SO4 (7% vol/vol) was mixed with methanol. The mixture was then
reacted with the rubber seed oil for 1hour, maintained at a temperature of 60oC and a stirring rate of 500rpm. This reduced the acid value of the rubber seed oil to 1.72 mg KOH/g oil.
Factorial experimental design, using the central composite design (CCD), was applied in the transesterification of the esterified seed oil. Thirty(30) experimental runs in which the esterified oil was reacted with methanol in the presence of K-
Pumice catalyst, were carried-out in a 250ml three-necked round bottom reactor, equipped with a reflux condenser and a hot plate with magnetic stirrer. The factors varied were; reaction time (90 to 180 minutes); methanol to oil ratio (6:1 to 10:1); K- Pumice catalyst (2 to 10% by weight of oil) and temperature (40oC to 60oC), while the agitation speed was set at 500rpm. At the end of reaction time, the biodiesel (rubber seed oil methyl ester) was placed in a rotary evaporator to remove excess methanol, and washed trice with deionized water at 50oC to
remove entrained glycerol. The washed biodiesel was then dried over anhydrous sodium sulphate at 50oC. The biodiesel yield was measured by the method described in [8]. The specific gravity; acid value; flash point and kinematic viscosity of the biodiesel were measured by the Association of Official Analytical Chemists methods [9]. Response surface method (RSM) was then used to optimize the transesterification process variables. The percentage yield of biodiesel was computed from Equation 1[8].
Biodiesel yield (%) = (%) x 100 Equation 1
In the kinetic analysis of the process, the biodiesel production was assumed to follow a single step reaction, as shown in Equation 2 [10]. The rate law expression can then be represented by Equation 3.
+ 3 + 3 Equation 2
= =
3 Equation 3
Where TG, ROH, G and E are triglyceride, methanol, glycerol and the fatty acid methyl ester (produced biodiesel). If the concentration of alcohol is considered to be in excess and the reverse reaction is ignored, then a pseudo first-order rate law can be written for the reaction as Equation 4 [10].
= =
Equation 4
1
Where K1 = 3
Also, due to the high methanol to oil ratio in the methanol phase, the rate law may be written in terms of TG only. If the reactio is assumed to be pseudo second-order, then the rate law can be expressed as Equation 5 [10].
= = 2 Equation 5
2
The pseudo First-order and Second- order kinetic models were then tested on the experimental data., while the effect of temperature on the reaction rate constant was modeled by the Arrhenius equation in Equation 6.
K = / Equation 6
In terms of conversion of triglyceride to biodiesel, Equation 4 can be written as Equation 7, which was integrated to give Equation 8.
d = – k1CTGO (1- XTG) Equation 7
-ln (1 XTG) = k1t Equation 8
The rate constant k1 was then determined from the plot of -ln (1 XTG) against time.
For the pseudo second- order kinetic model, the rate law in Equation 5 was written in terms of conversion as Equation 9, which
was integrated to give Equation 10. The rate constant K2 was then determined from the plot of 1
1
against time [10].
= k2CTGO2 (1 XTG)2
Equation 9
1
1
= k2CTGOt
Equation 10
The rate constants were evaluated at different temperatures, while the activation energy and pre-exponential factor were obtained from the Arrhenius plot of ln K against 1/T.
-
RESULTS AND DISCUSSION
-
Quadratic Model and Statistical Analysis of Biodiesel Production Process
Results obtained from the K-Pumice-catalyzed transesterification of the esterified rubber seed oil based on central composite experimental design are presented in Table 1. The Design expert software version 11 that was used generated the quadratic mathematical model shown in Equation 11. Equation 11 is the regression model in terms of actual process variables, and can be used to make predictions of the response for the given values of each factor.
An excellent correlation exists between the predicted yields and the experimental yields as shown in Figure 1 and Table 1. The coefficient of determination (R2) given as 0.9978 and the low
values of the residuals ( ± 0.42) are indicative of a well-fitted and reliable model. Analysis of variance (ANOVA) is reported in Table 2, while the Fit Statistics is reported in Table 3. From the ANOVA, all the process variables had positive effects on biodiesel yield, with the catalyst amount being the most influencing followed by temperature, reaction time and methanol to oil ratio respectively. The model terms are said to be significant if the p-value is less than 0.05. A p-value less than 0.0001 indicate that the model is significant. Also, the high F-value (475.5) implies that the model is significant.
Biodiesel yield (%) = -196.22292 + 0.473472 (Time) + 5.63333 (Temperature) + 5.83542 (Catalyst amount) + 19.66250 (Methanol to oil ratio) 0.001750 (Time)(Temperature) 0.007708 (Time)(Catalyst amount) +
0.018333 (Time)(Methanol to oil ratio) + 0.012500 (Temperature)(Catalyst amount) + 0.172500 (Temperature)(Methanol to oil ratio) 0.031250 (Catalyst amount)(Methanol to oil ratio) 0.001942 (Time2) 0.066917 (Temperature2) 0.361979 (Catalyst amount2) 1.88542 (Methanol to oil ratio2). Equation 11
Figure 1: Correlation of predicted biodiesel yield and actual biodiesel yield
Table 1: The experimental design and the actual and model predicted biodiesel yields
Run
Time (minutes)
Temperature (OC)
Catalyst amount (wt.%)
Methanol to
oil ratio (vol/vol)
Actual
biodiesel yield (%)
Predicted
biodiesel yield (%)
Residual
1
150
45
8
9:1
72.60
72.65
-0.05
2
150
55
8
7:1
73.00
73.00
0.00
3
90
55
8
7:1
74.30
74.34
-0.04
4
90
55
8
9:1
75.30
75.10
0.20
5
150
55
4
7:1
69.80
69.79
0.01
6
150
45
8
7:1
73.30
73.14
0.16
7
90
45
4
9:1
66.60
66.42
0.18
8
120
50
6
8:1
78.00
78.42
-0.42
9
120
60
6
8:1
73.40
73.59
-0.19
10
120
50
6
8:1
78.60
78.42
0.18
11
120
50
6
8:1
78.40
78.42
-0.02
12
90
55
4
9:1
70.20
70.29
-0.09
13
150
55
4
9:1
73.20
73.00
0.20
14
120
50
6
6:1
70.60
70.61
-0.01
15
180
50
6
8:1
72.50
72.64
-0.14
16
120
40
6
8:1
69.80
69.86
-0.06
17
120
50
6
8:1
78.50
78.42
0.08
18
90
45
8
9:1
70.80
70.74
0.06
19
120
50
2
8:1
68.70
68.86
-0.16
20
90
45
8
7:1
73.40
73.42
-0.02
21
150
55
8
9:1
76.10
75.97
0.13
22
90
45
4
7:1
68.80
68.85
-0.05
23
150
45
4
7:1
70.40
70.42
-0.02
24
120
50
6
8:1
78.20
78.42
-0.22
25
120
50
10
8:1
76.30
76.39
-0.09
26
60
50
6
8:1
70.10
70.21
-0.11
27
120
50
6
8:1
78.80
78.42
0.38
28
90
55
4
7:1
69.50
69.27
0.23
29
120
50
6
10:1
70.90
71.14
-0.24
30
150
45
4
9:1
70.30
70.19
0.11
Table 2: Analysis of variance for quadratic model
Source
Sum of squares
Degree of freedom
Mean square
F-value
p-value
Model
359.11
14
25.65
475.5
<0.0001
Significant
A- Time
8.88
1
8.88
164.64
<0.0001
B- Temperature
20.91
1
20.91
387.56
<0.0001
C- Catalyst amount
85.13
1
85.13
1578.04
<0.0001
D- Methanol to oil ratio
0.4267
1
0.4267
7.91
0.0131
AB
1.10
1
1.10
20.44
0.0004
AC
3.42
1
3.42
63.44
<0.0001
AD
4.84
1
4.84
89.72
<0.0001
BC
0.2500
1
0.2500
4.63
0.0480
BD
11.90
1
11.90
220.64
<0.0001
CD
0.0625
1
0.0625
1.16
0.2988
A2
83.80
1
83.80
1553.45
<0.0001
B2
76.76
1
76.76
1423.00
<0.0001
C2
57.50
1
57.50
1065.97
<0.0001
D2
97.50
1
97.50
1807.47
<0.0001
Residual
0.8092
15
0.0539
Lack of fit
0.4008
10
0.0401
0.4908
0.8417
Not significant
Pure error
0.4083
5
0.0817
Correlated total
359.91
29
Table 3: Fit statistics for quadratic model
Statistical parameter
Value
Standard deviation
0.2323
Mean of response
73.01
Coefficient of variance (%)
0.3181
R2
0.9978
Adjusted R2
0.9957
Predicted R2
0.9920
Adequate precision
73.0419
In Table 3, the difference between Adjusted R2 and Predicted R2 (0.0037) is lower than the allowable difference of 0.2, indicating that the model can predict the response of the process within acceptable range. The adequate precision value of 73.0419 is also higher than the critical value of 4, again indicating that the model can navigate the design space for the optimization purpose [8].
-
Effect of Interacting Factors on Biodiesel Yield
The 3D plots of the interacting effects between process variables on the biodiesel yield are given in Figure 2 (a) to (f). The 3D-surface plot depicted in Figure 2 (a) shows the interaction between temperature and reaction time, with the catalyst amount and the methanol to oil ratio kept constant. Simultaneous increase in temperature and reaction time resulted in a corresponding increase in the biodiesel yield. This is because of the better mixing of rubber seed oil and methanol as temperature increased. However, at an optimum reaction time of 150 minutes, increase in the reaction temperature above 55oC led to a decrease in biodiesel yield. The optimum temperature for the biodiesel production process was found to be 55oC. Studies have shown that when temperature increases beyond the
optimal temperature, the yield of biodiesel decreases due to acceleration of the saponification reaction of the triglyceride ([11]; [12]). An optimum temperature of 45 ± 5 for biodiesel production from Rubber seed oil was reported in [13], while in another study [14], a reaction temperature of 60oC was observed as the optimum.
Figure 2 (b) shows the interaction between catalyst amount and reaction time, with the reaction temperature and the methanol to oil ratio kept constant. There is an observed increase in the yield of biodiesel when the catalyst amount and reaction time are simultaneously increased. An optimum biodiesel yield of 75.97% was observed at a reaction time of 150 minutes. It could be observed from Figure 2 (c) to (f) that, simultaneously increasing the interacting variables resulted in increase in the biodiesel yield. However, increasing these variables beyond their optimal values resulted in a decrease in biodiesel yield [15]. In addition to affecting the yield of biodiesel, the catalyst amount also influences its colour. The higher the amount of catalyst, the darker the biodiesel produced. Therefore, the addition of a suitable amount of catalyst is important to the physical appearance of biodiesel [13]. Table 4 shows the
Published by :
optimum value of each process variable for the biodiesel production process. The optimum temperature was found to be 55oC; while 150 minutes, 8 wt.% and a ratio of 9:1, were the optimum values for time, catalyst amount and methanol to oil ratio respectively. The optimum biodiesel yield was 75.97%.
Table 4: Optimized values
International Journal of Engineering Research & Technology (IJERT)
ISSN: 2278-0181
Vol. 13 Issue 07, July-2024
Parameter
Value
Time (minutes)
150
Temperature (degree Celsius)
55
Catalyst amount (wt. %)
8
Methanol to oil ratio (vol/vol)
9:1
Biodiesel yield (%)
75.97
(a) Temperature and Time (b) Catalyst amount and Time
-
Catalyst amount and Temperature
-
Methanol to oil ratio and Time
-
Methanol to oil ratio and Temperature (f) Methanol to oil ratio and Catalyst amount
Figure 2: 3D plots for the interactive effects between process variables on biodiesel yield.
IJERTV13IS070018
(This work is licensed under a Creative Commons Attribution 4.0 International License.)
-
-
Kinetics
-
Kinetic Model
In Table 5, the R-square values for the rate law plots are presented for the pseudo first-order and the pseudo second- order kinetic models. The plots were obtained by varying the temperature and the reaction time, while keeping the catalyst amount and methanol to oil ratio at their optimum values of 8
wt.% and 9:1 vol./vol. respectively. From the R-square values, both kinetic models appear to fit the reaction data, but the pseudo second-order kinetic model which gave a higher R- square value for all the temperatures considered, described the reaction better. Hence, further kinetic evaluations were based on the pseudo second-order model.
Table 5. Values of R-square for rate law plots at different temperatures
Tremperature (oC)
Pseudo first-order model
Pseudo second-order model
40
0.9669
0.9775
45
0.9637
0.9759
50
0.9596
0.9732
55
0.9525
0.9663
60
0.9410
0.9540
-
Rate Constants, Pre-exponential Factors, Activation Energy and Rate Law
Values of the rate constants k at temperatures ranging from 40 OC to 60 OC are shown in Table 6, the rate laws at these temperatures are presented in Table 7, while the Arrhenius plot from the biodiesel production process is given in Figure 3. It is observed from Table 3, that the rate constant increased with temperature up
to 55 OC, and then decreased thereafter. Indicating that the rate of formation of biodiesel increased with temperature up to an optimum of 55 OC, but reduced beyond this temperature. The Arrhenius plot of Figure 3 covers the temperatures range 40 OC and 55 OC. The activation energy Ea was computed to be 39.030 KJmol-1, while the pre-exponential factor A, was calculated to be
3.93 x 104.
Table 6: Values of rate constant, k at various temperatures
Temperature, oC (Kelvin)
Rate constant (k)
ln k
1/T (K-1)
40 (313)
0.0111
-4.5008
3.195 x 10-3
45 (318)
0.0160
-4.1352
3.145 x 10-3
50 (323)
0.0198
-3.9221
3.096 x 10-3
55 (328)
0.0221
-3.8122
3.049 x 10-3
60 (333)
0.0159
-4.1414
3.003 x 10-3
IJERTV13IS070018
(This work is licensed under a Creative Commons Attribution 4.0 International License.)
-3.7
1/T
0.003 0.00305 0.0031 0.00315 0.0032 0.00325
-3.8
-3.9
-4
Ln K
-4.1
-4.2
-4.3
-4.4
-4.5
-4.6
y = -4694.5x + 10.56 R² = 0.9466
Figure 3: Arrhenius plot of ln k against 1/T for the biodiesel production process
Table 7: Rate law at various temperatures
Temperature, oC (Kelvin)
Rate law
40 (313)
2
-rA = 0.0111 CA
45 (318)
2
-rA = 0.0160 CA
50 (323)
2
-rA = 0.0198 CA
55 (328)
-rA = 0.0221 C 2
A
60 (333)
-rA = 0.0159 C 2
A
-
-
Characterization of Biodiesel
The specific gravity, acid value, kinematic viscosity and flashpoint of the biodiesel produced were characterized by following ASTM procedures. The values obtained were compared with literature values of biodiesel synthesized from rubber seed oil, as well as the ASTM D 6751 biodiesel standard. The results are presented in Table 8. The properties of the biodiesel obtained in the current study compared favourably with those from similar studies on biodiesel production from rubber seed oil, and were in agreement with the ASTM D 6751 biodiesel standard.
Table 8: Comparison of some properties of the produced biodiesel with those from other works
Properties
Specific gravity
Acid value (mgKOH/g oil)
Flash point (oC)
Kinematic viscosity at 40oC (mm2/s)
ASTM Standard values
0.86 0.9
< 0.6
100 170
1.9 6
[13] 0.874
0.118
130
5.81
[16] 0.85
0.12
120
4.5
[17] 0.885
0.42
152
3.89
[18] 0.87
0.07
154.6
4.64
[8] 0.876
0.56
158
4.32
[15] 0.88
0.26
140
4.49
Present study
0.87
0.43
150
5.0
-
-
CONCLUSION
The production of biodiesel from a low-cost, non-edible feedstock, rubber seed oil, was investigated. The biodiesel yield was affected by reaction time, temperature, catalyst amount and methanol to oil ratio. Increase in each of these variables led to a corresponding increase in the yield of biodiesel. However, beyond the optimum values of 150 minutes, 55oC, 8 wt.% of oil and 9:1 vol/vol for reaction time, temperature, catalyst amount and methanol to oil ratio, there was an observed decrease in the yield of biodiesel. The optimum yield of biodiesel was found to be 75.97%. A quadratic model for the biodiesel production
process was derived. The model is suitable for the prediction of biodiesel yield. The kinetics of rubber seed oil transesterification was also investigated. The reaction was found to fit a pseudo second-order model, based on this, the rate constants at various temperatures, the activation energy and the pre-exponential factor were obtained. The determined physical properties of the produced biodiesel, compared favourably with those from other studies. K-Pumice catalyst has shown to be an effective catalyst for the synthesis of biodiesel from rubber seed oil.
IJERTV13IS070018
(This work is licensed under a Creative Commons Attribution 4.0 International License.)
REFERENCES
-
Onoji, S. E., Iyuke, S. E., Igbafe, A. I. and Nkazi, D. B. (2016a). Rubber seed oil: A potential renewable source of biodiesel for sustainable development in sub-Saharan Africa. Energy Conversion and Management, 110, 125 134.
-
Gimbun, J., Ali, S., Kanwal, C. C. S. C., Shah, L. A., Ghazali, N. H. M., Cheng, C. K. and Nurdin, S. (2013).Biodiesel production from rubber seed oil using activated cement clinker as catalyst.Procedia Engineering, 53: 13 19.
-
Demirbas, A. (2009). Progress and recent trends in biodiesel fuels.Energy Conversion and Management, 50: 14-34.
-
Cercado, A. P., Ballesteros Jr, F. and Capareda, S. (2018). Ultrasound assisted transesterificationof microalgae using synthesized novel catalyst. Sustainable Environment Research, 28: 234-239.
-
Meher, L. C., Sagar, D. V. and Naik, S. N. (006). Technical aspects of biodiesel by transesterification: A review. Renewable and Sustainable Energy Reviews, 10(3): 248 268.
-
Kouassi, K. E., Abolle, A., Yao, K. B., Boa, D., Adouby, K., Drogui, P. and Tyagi, R. D. (2018).Optimization of rubber seed oil transesterification to biodiesel using experimental designs and artificial neural networks.Green and Sustainable Chemistry, 8: 39 61.
-
Aransiola, E.F., Betiku, E., Ikhuomoregbe, D.I.O. and Ojumu, T.V. (2012). Production of biodiesel from crude neem oil feedstock and its emissions from internal combustion engines. African Journal of Biotechnology, 11(22): 6178 6186.
-
Onoji, S. E., Iyuke, S. E., Igbafe, A. I. and Daramola, M. O. (2017).Transesterification of rubber seed oil to biodiesel over a calcined waste rubber seed shell catalyst: Modeling and optimization of process variables. Energy & Fuels, 31(6): 6109 6119.
-
Association of Official Analytical Chemist (A.O.A.C.) (1990). Official methods of analysis. 15th Edition. Washinton DC
-
Feyzi M. and Khajavia G. (2016). Kinetic study of biodoesel synthesis from sunflower oil using Ba-Sr/ZSM-5nanocatalyst. Iranian Journal of Catalysis 6(1): 29-35
-
Leung D. Y. C and Guo Y. (2006). Transexterification of neat and used frying oil: Optimization for biodiesel production. Fuel processing technology, 87(10):
883-890
-
Hadiyanto, H., Widayat, W. and Duma, A. (2016). Ultrasound assisted in situ esterification of rubber seed oil for biodiesel production. International Journal of Engineering, 29(12): 1635 1641.
-
Ramadhas, A. S., Jayaraj, S. and Muraleedharan, C. (2005). Biodiesel production from high FFA rubber seed oil. Fuel, 84: 335 340.
-
Abdulkadir, B. A., Uemura, Y., Ramli, A., Osman, N. B., Kusakabe, K. and Takami, K. (2015).Production of biodiesel from rubber seeds (HeveaBrasiliensis) by in situ transesterification method. Journal of the Japan Institute of Energy, 94: 763 768.
-
Bharadwaj, A. V. S. L., Singh, M., Niju, S., Begum, K. M.
M. S. and Anantharaman, N. (2019).Biodiesel production from rubber seed oil using calcium oxide derived from eggshell as catalyst optimization and modeling studies. Green Processing and Synthesis, 8: 430 442.
-
Morshed, M., Ferdous, K., Khan, M. R., Mazumder, M. S. I., Islam,
M. A. and Uddin, M. T. (2011). Rubber seed oil as a potential source for biodiesel production in Bangladesh.Fuel, 90: 2981 2986.
-
Ahmad, J., Suzana, Y., Awais, B. and Ruzaimah, N. M. K. (2014b). Study of fuel properties of rubber seed oil-based biodiesel. Energy Conversion and Management, 78: 266 275.
-
Hussain, S., Ali, S., Ahmed, I., Gimbun, J. and Muhammad, H.
A. (2016). Microwave reinforced transesterification of rubber seed oil using waste cement clinker catalyst. Current Nanoscience, 12: 1 10.
IJERTV13IS070018
(This work is licensed under a Creative Commons Attribution 4.0 International License.)