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7/27/2019 Balakrishnan Paper Ieee Format

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and purificationfrom the trace compounds. The upper phase

mainly contains methyl/ethyl ester, whichafter removing an

excess of methanol and washing with water is used asbiodiesel. Then it is characterized to meet the ASTM

requirements and the biodiesel yield is compared.

Transesterification reaction is shown in fig. 1.

Fig.1. Transesterification reaction

2. METHODS

2.1MaterialsThe primary raw materials of Pongamia oil was used in

the production of biodiesel. Pongamia oil was collected from a

local market. These materials contain triglycerides, free fatty

acids, and other contaminants. Since biodiesel is a mono-

alkyl fatty acid ester, the primary alcohol used to form the

ester is the other major feedstock. Methanol was obtained

from Taleco Laboratory for the Transesterification. Most

processes for making biodiesel use a catalyst to initiate the

esterification reaction. The catalyst is required because the

alcohol is sparingly soluble in the oil phase. The catalyst

promotes an increase in solubility to allow the reaction to

proceed at a reasonable rate. Sulphuric acid was obtained fromthe Laboratory for the transesterification process.

2.2EquipmentReactor consists of spherical flask of 1L capacity, which

is put inside the heat jacket. Water is used as a medium of heat

transfer from heat jacket to the reactor. Thermostat is a part of

heat jacket, which maintains the temperature of water and inturn the temperature of the reactants at a desired value. The

reaction is carried out at around 55-70C. Spherical flask

consists of three openings. The centre one is used for putting

stirrer in the reactor. The motor propels the stirrer.

Thermometer is put inside the second opening to continuously

monitor the temperature of the reaction. Condenser is put in

the third opening to reflux the alcohol vapours back to the

reactor to prevent any reactant loss. Batch reactors have

several positive features including good mixing characteristics

and relativeease of handling homogeneous catalysts as used in

the biodiesel transesterification reaction.

2.3Experimental ProcedureThe reactor was initially filled with the desired amount

ofPongamiaoil, then placed in the constant-temperature bath

withits associated equipment and heated to a

predeterminedtemperature of 65C. The catalyst H2SO4was

dissolved in the methanoland the resulting solution was added

to the agitated reactor.The reaction was timed as soon as the

catalyst/methanolsolution was added to the reactor and itcontinued for3hrs. Then the mixture was transferred to a

separatory funnel,allowing glycerol to separate by gravity for

4 hrs. Afterremoving the glycerol layer, the acidic methyl

ester layer was changed to alkaline methyl ester when methyl

ester was washed with mixture of NaHCO3and water.Then

alkaline methyl ester was washed with mixture of NaCl andwaterto remove methanol, catalyst and glycerol residuals. The

methyl esterphase was then analysed to calculate the biodiesel

yield. The resulting biodiesel was characterized for its fuel

properties. Biodiesel production process flow is shown in fig 2.

Fig.2. Batch Reaction Process

3. RESULTS AND DISCUSSION

3.1Analysisof feedstock

The physical and fuel properties of Pongamiaoil are

measured and compared with Diesel below,

Table 1. Physiochemical properties of oils

Properties Pongamia

oil

Diesel

Specific gravity @15/150C 0.9413 0.8225

Kinematic viscosity @40C

in cSt

51.5 3.01

Flash point (oC) 243 51

Fire point (oC) 255 61

Cloud point +9 +8

Pour point +1 -13

Gross calorific value in

kcal/kg

9,976 10713

Cetane Number 49.8 51

Density @15 C in gm / cc 0.9405 0.8218


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Kinematic viscosity of oil is very higher than the

diesel. The diesel engine does not run the high viscosity.

Hence viscosity is reduced in biodiesel production process.

Flash point and fire point are higher than the diesel. Itis used to the transportation safety.

The specific Gravity of conventional diesel fuel is

about 0.8225 while a typical specific Gravity of Pongamia oil

is 0.9413, which means Pongamia oil is denser than

conventional diesel fuel.

3.2. Effect of reaction time on feedstocks conversion

Effect of reaction time on Pongamia oil conversion is shown

in fig 3.The conversion rate increases with time. The di

glycerides and mono glycerides increased at the beginning and

then decreased with increase in time duration. At the end of

transesterification the amount of mono glycerides should be

higher than that of triglycerides. In this project time duration

is varied from 3 to 6 hours.

Fig. 3. Effect of reaction time

3.3 Effect of molar ratio on feedstocks Conversion

Fig 4.Shows the effect of molar ratio of methanol to

Triglyceride on the Pongamia oil conversion into Methyl

Ester.The stoichiometric ratio for the transesterification

requires three moles of alcohol and one mole of triglyceride toyield three moles of fatty acid methyl ester and one mole of

glycerol. However transesterification is an equilibrium

reaction in which a large excess of alcohol is required to drive

the reaction to the right side. For maximum conversion of

ester greater than 6:1 molar ratio is used. The molar ratio hasno effect on acid, peroxide, saponification and iodine value of

methyl esters. However the high molar ratio of alcohol to

vegetable oil interferes the separation of glycerol because of

increase in solubility. When the glycerol remains in the

solution it helps to drive the equilibrium to the left side

lowering the yield of esters. Methanol and ethanol are not

miscible with triglycerides at room temperature and the

reaction mixtures are mechanically stirred to enhance mass

transfer. During the course of reaction emulsions usually form.

In case of methanolysis these emulsions quickly and easily

breakdown to form a lower layer glycerol and upper rich layer

of methyl ester. In ethanolysis these emulsions are more stable

and severely complicate the separation and purification of

esters. In this project molar ratio is varied from 3:1 to 12:1.

Fig.4. Effect of molar ratio

3.4. Effect of reaction temperature on feedstocks conversionAs ageneral rule, transesterification reaction is tried to be

accomplished at lowest possible temperature. The commonly

employed temperature ranges from as low as room

temperature to up to 65C. Transesterification reaction has

been reported to be influenced positively with increase in

temperature. The boiling point of methanol is 64.7C and

hence the transesterification reaction is carried out within this

range of temperature higher than this may burn methanol. In

this project reaction temperature is varied from 550C to 70

0C.

Higher conversion rate is obtained at 650C. More conversion

rate can be achieved at higher temperature but it is not triedowing to danger of methanol vapours. Since temperature

increases viscosity reduces. Lower temperatures are notsuitable for transesterification reaction because of higher

viscosity. Hence 650C temperature is kept fixed. Effect of

amount of catalyst on Pongamia oil conversion is shown in fig

5.

Fig. 5.Effect of reaction temperature

3.4 Effect of amount of catalyst on feedstocks conversion

Higher the acidity of the oil, smaller the conversion efficiency.

The addition of more amount of catalyst compensates for

higher acidity, but the resulting soap causes an increase in

85.586

86.587

87.588

88.589

89.5

2 3 4 5

Reaction time (hrs)

MethylEster%

8585.5

8686.5

8787.5

8888.5

89

3 6 9 12

molar ratio

MethylEste

r%

86.5

87

87.5

88

88.5

89

55 60 65 70

amount of catalyst %

methylester%


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viscosity or formation of gels which interferes the reaction as

well as separation of glycerol. When the reaction conditions

do not meet the above requirements ester yields aresignificantly reduced. In this project catalyst concentration is

varied from 1.0 wt% to 2.5wt%. Maximum conversion

efficiency is obtained at 1.5wt% and there is a significant

reduction at 2.0 wt% because of excess catalyst lead to the

formation of soap and decreased the yield.Effect of amount ofcatalyst on PongamiaOil conversion is shown in fig 5.

Fig. 5. Effect of catalyst concentration

3.6 Characterization of methyl esters

Methyl ester ofPongamia oil and diesel has different varying

origin and quality. Hence, variation in the physical properties

of biodiesel based on its oil source is obvious. Irrespective of

the oil source, the biodiesel quality should meet certain

standards in order to ensure better engine performance.

American Society for Testing and Materials (ASTM) standard

must be met in order to characterize the Biodiesel as a fuel.

The acceptable Viscosities for biodiesel are nearly similar to

that of the diesel fuel.

The Biodiesel were characterized by determining its density,

viscosity, higher heating value (HHV), cloud and pour points,

characteristics of distillation and flash and combustion points

according to meet the standards. The fuels were characterized

by evaluation of the parameters required in ASTM, orAmerican Standard Test Materials. The Biodiesel esters were

characterized for their physical and fuel properties. The

viscosities of Biodiesel fuels are twice compare to petroleum

diesel. The cloud and pour points of petroleum diesel are

significantly lower than those of the Biodiesel fuels. Biodiesel

is aclean, 100% natural energy alternative to petroleum

fuels.Table 4. Shows the fuel properties of biodiesel produced

from Pongamia oil. All the values were within the ASTM

standard limits.

Table 4. Fuel Properties of Methyl esters

Parameter Pongamia

oil

Biodiesel

from

Pongamia

oil

Diesel

Specific gravity

@15/150C

0.9413 0.889 0.8225

Kinematic viscosity

@40C in cSt

51.5 9.9 3.01

Flash point (oC) 243 192 51

Fire point (oC) 255 203 61

Cloud point +9 +9 +8

Pour point +1 +1 -13

Gross calorificvalue in kcal/kg 9,976 10189 10713

Cetane Number 49.8 50 51

Density @15 C in

gm / cc

0.9405 0.881 0.8218

4. CONCLUSION

Pongamiaoil is an economical feedstock for the production of

biodiesel. However, the production process using this

feedstock is usually more complicated than that using fresh oil

feedstock. Due to the reduction of feedstock cost compared to

other edible and non edible oils, biodiesel fromhighlyPongamia oil is a promising alternative.

The SFC increases with increase in percentage of biodiesel inthe blends due to the lower heating value of biodiesel. The

BTE of biodiesel and its blends are slightly higher than that of

diesel at high engine loads, and keep almost same at lower

engine loads.

combustion and increases the combustion chamber

temperature, which leads to higher NOx emissions, especially

at high engine loads. The significant improvement in

reduction of NOx and a minor increase in CO2 were identified

use of selective catalytic reduction (SCR).

difference from diesel fuel. It is also observed that there is a

significant reduction in CO and smoke emissions at high

engine loads.

biodiesel play a key role in engine performance and biodiesel

is proved to be a potential fuel for complete or partially

replacement of diesel fuel. The combustion starts earlier for

biodiesel and its blends than for diesel. The peak

cylinderpressure of biodiesel and its blends is higher than that

86.5

87

87.5

88

88.5

89

89.5

1 1.5 2 2.5

amount of catalyst %

methylester%


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of diesel fuel, and almost identical at high engine loads. The

peak pressure rise rate and peak heat release rate of biodiesel

are higher than those of diesel fuel

ACKNOWLEDGEMENT

A moral support from CLRI, Chennai for providing all the

adequate facilities for producing biodiesel from Pongamia oil

is greatly acknowledged.

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