Unrefined rice bran
oil (UNRFRBO) with high free fatty acids (FFA) is used as a source for the production
of unrefined rice bran oil methyl ester (UNRFRBOME). Three-stage transesterification
process is successfully used. Initially, the FFA of UNRFRBO is reduced to 1%
(0.8%) by using two stages esterification process with methanol in the presence
of acid (H2SO4) as a catalyst. Finally, biodiesel has
produced by alkaline (NaOH) catalyzed transesterification process which has designed
according to the central composite design. 90% has obtained at the optimum values
of CH3OH (20% v/v of oil), NaOH (1.0% w/v of oil), reaction time (60
minutes) and reaction temperature (55°C to 60°C).
Due to clean emission profile, ease of use and other benefits biodiesel quickly become one of the fastest growing alternative fuels in the world.
The future of biodiesel lies in the world’s ability to produce renewable feedstock such as vegetable and ani- mal oils, to keep the cost of biodiesel competitive with petroleum.
The rice bran oil is extracted from the rice bran, which is a byproduct obtained during the grinding of paddy. Since rice is the staple food in a large part of south Asia, there is a huge potential to produce and utilize rice bran oil. India is the second largest producer of paddy. Hardly 50% of the bran is utilized for producing rice bran oil and 19% of edible grade rice bran oil is consumed for cooking, hence Rice bran oil is commercially feasible for biodiesel production.
Rice bran oil is a byproduct obtained from outer layers of brown rice kernel during milling operation to pro- duce polished rice. Rice bran has 16 wt% to 32 wt% [1] oil (lipids) and nutraceutical compounds are depending on the rice variety and degree of milling.
Crude RBO is difficult to refine because of its high free fatty acid contents, dark color, and a large amount of un-saponifiable matter. FFA content as high as 4% to 8% has been found [1] in the oil that has obtained from bran immediately after milling of rice.
Few researchers [2] -[4] investigated biodiesel production from crude RBO by alkaline catalyzed transesteri- fication process. However, possibility of soap formation increases with the use of this method as its FFA level found to be more than 1% and finally it affects the quality and quantity of biodiesel. Many researchers [5] [6] used acid catalyzed transesterification process for biodiesel production from RBO and conducted a series of ex- periments at 1:10 molar ratio of oil/methanol, 2 wt% H2SO4, and reaction temperature of 60˚C for a wide range of FFA. Researchers found that biodiesel yield decreased with an increase in FFA level. Considerable research has also been done on biodiesel production from RBO by using two-stage transesterification and lipase cata- lyzed transesterification process. Alcoholysis of crude RBO can be achieved under mild reaction conditions and in short reaction times in the presence of lipases. Lipase catalyzed transesterification allows easy recovery of glycerol with any purification method. In this work, an attempt has been made to use three-stage transesterification processes to convert UNRFRBO into UNRFRBOME.
The below figure represent the three-stage transesterification process for the unrefined ricebrane oil.
2. Materials
Required quantity of UNRFRBO is purchased from a rice mill near Tumkur, Karnataka State, India. All chemi- cals such as methanol (99.5% purity), H2SO4 (99% purity), NaOH pellets have purchased from VASA scientific company, Bangalore, Karnataka State, India. All chemicals were of analytical grade.
2.1. Characterization of UNRFRBO
Fatty acid composition of UNRFRBO.
Table 1 shows the fatty acid composition of UNRFRBO.
2.2. Physical Properties of UNRFRBO
Table 2 shows physical properties of UNRFRBO. UNRFRBO has a higher amount of FFA (8%) which is above the accepted limit (i.e., 1%) for alkaline catalyst transesterification process. Therefore, in this work pretreatment stages have used to convert FFA into esters by treating UNRFRBO with methanol in the presence of an acidic catalyst (H2SO4, 0.5% v/v) to bring the FFA amount to less than 1%. Finally, transesterification process is com- pleted by using an alkaline catalyst.
3. Stage 1 Acid Catalyzed Esterification Process
In this stage, nine experiments have conducted by varying methanol quantity (2.5%, 5%, and 7.5% v/v of oil) and reaction time (45 min, 60 min, and 75 min). Experiments were conducted by keeping acid catalyst concen- tration (H2SO4, 0.5% v/v) and reaction temperature (55˚C to 60˚C) constant.
3.1. Experimental Procedure
UNRFRBO has taken into the reactor. Water bath temperature is maintained at 55˚C to 60˚C. Required amount of CH3OH added to the concentrated H2SO4 (0.5% v/v of oil). The mixture slowly added to the heated oil. Stir- ring at low RPM and heating (55˚C to 60˚C) is continued for different reaction times. Similar methods were used for all nine experiments which were conducted according to the experimental matrix shown in Table 3. On completion of reaction, the mixtures were allowed to fall into two layers. The excess methanol, H2SO4, and im- purities moved to the top surface and were taken out. The acid value of the product separated at the bottom is measured.
Table 3 shows the FFA level for different combination of CH3OH and reaction time for UNRFRBO for Stage-1 acid catalyzed transesterification process.
Table 1
. Fatty acid composition of UNRFRBO
Sl. No
Components
UNRFRBO (% by weight)
1
Palmitic acid (16:0)
20.12
2
Stearic acid (18:0)
2.8
3
Oleic acid (18:1)
40
4
Linoleic acid (18:2)
30
5
Linolenic acid (18:3)
2.5
Table 2
. Physical properties of UNRFRBO
Sl. No
Properties
Unit
RBO
1
Viscosity at 40˚C
cSt
12.3
2
Density
kg/m3
914
3
Flash point
˚C
260
4
Calorific value
MJ/kg
36.16
5
Pour point
˚C
−5
Table 3
. Layout of experimental design and results for Stage-1 acid catalyzed transesterification process
Experiment No
Samples
CH3OH (% v/v of oil)
Reaction time in minutes
FFA (%)
1
S1
2.5
45
6.5
2
S2
2.5
60
5
3
S3
2.5
75
3.5
4
S4
5
45
3.8
5
S5
5
60
2.5
6
S6
5
75
2
7
S7
7.5
45
2.2
8
S8
7.5
60
1.8
9
S9
7.5
75
2.2
3.2. Stage 2 Acid Catalyzed Esterification Process
Sample (S8) has selected as a source for this stage because it has minimal FFA level (1.8%). Table shows the experimental conditions for Stage 2 acid catalyzed transesterification process. In this stage also, nine experi- ments have conducted by varying methanol quantity (2%, 4%, and 6% v/v of oil) and reaction time (45 min, 60 min, and 75 min) according to the experimental matrix shown in Table 4. Experiments have conducted by keeping acid catalyst concentration (H2SO4, 0.5% v/v) and reaction temperature (55˚C to 60˚C) constant. Expe- riments were conducted by using the procedure that has used for stage 1 acid catalyzed esterification process. The acid value of the product at the bottom is measured. The product having minimum FFA level is chosen as a source for the third stage.
3.3. Stage 3 Alkaline Catalyzed Transesterification Process
Sample (S88) has selected as a source for alkaline catalyzed transesterification process as its FFA amount less than 1% (i.e., 0.6%).
3.4. Experimental Procedure
Sample (S88) (Table 4) has taken into the reactor. Water bath is maintained at 55˚C to 60˚C temperature. Sodium methoxide solution is prepared by dissolving required amount of NaOH in desired amount of CH3OH. Half of the prepared sodium methoxide solution slowly added to the heated oil. Stirring and heating continued for 10 to 15 minutes. Then, remaining half of the prepared sodium methoxide solution slowly added to the heated mix- ture.
Stirring at low RPM and heating (55˚C to 60˚C) is continued for another 45 minutes to 50 minutes (i.e., total reaction time of 60 minutes). Similar method has used for all 12 experiments which have conducted according to the experimental matrix shown in Table 5. On completion of reaction, the mixtures allowed to fall into two lay- ers with the UNRFRBO on the top and glycerol on the bottom. The raw UNRFRBOME collected, and water washed twice to bring the pH of UNRFRBOME to 7.
4. Results and Discussion4.1. Stage 1 Acid Catalyzed Esterification Process
Figure 1 shows that the effect of methanol quantity and reaction time on FFA level of UNRFRBO. Figure shows that the reaction progressed rapidly in the initial stage and became slower in the later phase. It also shows that the FFA level steadily decreased with an increase in the quantity of methanol at the same period of reaction time. Sample S8 has minimum FFA (1.8%) at the optimized methanol quantity of 7.5% v/v of oil and reaction time (60 minutes). Sample (S8) has used for Stage 2 acid catalyzed esterification process.
Table 4
. Layout of experimental design and results for Stage 2 acid catalyzed transesterification process
Experiment No
Type of feedstock
Samples
CH3OH (% v/v of oil)
Reaction time in minutes
FFA (%)
1
Sample S8
S81
2
45
1.6
2
S82
2
60
1.4
3
S83
2
75
1.5
4
S84
4
45
1.3
5
S85
4
60
0.8
6
S86
4
75
1.1
7
S87
6
45
1.2
8
S88
6
60
0.6
9
S89
6
75
1
Table 5
. Experimental matrix and experimental results
Exp. No
CH3OH (% v/v of oil)
NaOH (% w/v of oil)
Biodiesel yield (% v/v of oil)
1
15
0.5
80.2
2
25
0.5
82.1
3
15
1.5
70.5
4
25
1.5
65.5
5
20
1.0
85.5
6
20
1.0
85.0
7
20
1.0
85.2
8
20
1.0
85.2
9
20
1.84
60.3
10
28.4
1.0
63.3
11
11.6
1.0
60.4
12
20
0.16
78.5
Influence of quantity of methanol and reaction time on FFA level of UNRFRBO
4.2. Stage 2 Acid Catalyzed Esterification Process
Figure 2 shows the effect of the molar ratio of methanol to oil and reaction time on FFA level of sample S8. It
Influence of quantity of methanol and reaction time on FFA level of sample S8
can be seen from the Figure that the reaction time showed the same trend as in case of the first stage. Sample S88 has minimum FFA (0.6%) at the optimized methanol quantity 6% v/v of oil and reaction time (60 minutes). Sample (S88) has selected for Stage 3 (alkaline catalyzed) esterification process.
4.3. Stage 3 Alkaline Catalyzed Transesterification Process
Alkaline catalyzed transesterification reaction is conducted using the pretreated S88 with FFA level of 0.6%. In order to get the optimal conditions for maximum UNRFRBOME yield, experiments have been conducted ac- cording to CCD experimental matrix (Table 5).
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