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Cosolvent Transesterification of Jatropha Curcas Seed Oil


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Cosolvent Transesterification of Jatropha Curcas Seed Oil

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  • 1. Journal of Petroleum Technology and Alternative Fuels Vol. 3(4), pp. 42-51, April 2012Available online at 10.5897/JPTAF11.038©2012 Academic JournalsFull Length Research PaperCosolvent transesterification of Jatropha curcas seed oil I. A. Mohammed-Dabo1*, M. S. Ahmad2, A. Hamza1, K. Muazu3 and A. Aliyu1 1 Chemical Engineering Department, Ahmadu Bello University Zaria, Nigeria. 2 Center for Renewable Energy Research, Umaru Musa Yarádua University, Katsina, Nigeria. 3 National Research Institute for Chemical Technology Zaria, Nigeria. Accepted 7 March, 2012 This is paper aimed at characterizing Nigerian Jatropha curcas seed oil in terms of % free fatty acid (FFA), viscosity, calorific, acid, iodine and saponification values and cetane number which were found to conform to those in literature. The GC-MS analysis of the raw oil indicated that oil consisted principally of palmitic, oleic, linoleic and stearic acids. The established operating conditions for the efficient cosolvent transesterification of Jatropha oil, using tetrahydrofuran as the cosolvent, were found to be 40°C, 200 rpm, 4:1 methanol-to-oil molar ratio, 1:1 cosolvent-to-methanol volume ratio, 0.5% w/w catalyst concentration and a time duration of 10 min. An optimum yield of 98% was obtained at these conditions and the result of the GC-MS analysis confirms the formation of methyl ester at these conditions. Properties of the biodiesel obtained at these optimum transestrification conditions were compared favourably with the ASTM D 6751-02 Standard B100. Key words: Jatropha curcas, transesterification, cosolvent, biodiesel.INTRODUCTIONThe three dimensional energy threat of climate change, potential to get as much as 1,600 gallons of diesel fuelaffordability and energy security has lead the world to per acre in a year. J. curcas tree can also bediscover the finite nature of fossil fuels, even though they intercropped with other cash crops such as coffee, sugar,will continue to dominate the global primary energy mix fruits and vegetables.for several decades to come (World Energy Outlook, Biodiesel production through transesterification process2009; Meda et al., 2009). Growth in world population has involves reaction of the oil with an alcohol (mostlyresulted into surge in energy demand, and therefore the methanol) in the presence of a catalyst resulting into theneed for secured energy source that are renewable, formation of a diesel equivalent biofuel (mono alkylenvironmentally friendly, affordable and above all ester). This transesterification process is associated withsustainable has arise. Various feedstocks have been many problems, in which the principal of these problemsproposed for the production of biodiesesl, one of the is that the reactants (oils and alcohols) are not readilycontending candidates is the Jatropha curcas. This tree is miscible because of their chemical structures. Oilselected due to its numerous advantages over others. J. disperses in the methanol medium, so the rate of collisioncurcas is non-edible as it contains compounds that are of the glyceride and the methoxide (the mixture ofhighly toxic. It is resistant to drought and pests. Seed methanol and the alkaline catalyst – KOH or NaOH)yields under cultivation can range from 1,500 to 2,000 kg molecules becomes slower. This lowers the rate of -1ha , corresponding to extractable oil yields of 540 to 680 collisions of the molecules and also the rate of reaction -1L ha (58 to 73 US gallons per acre) and they have the causing longer reaction times, higher operating expenses and labour, higher fixed capital investments and consequently higher product costs (Caglar, 2007). To overcome this difficulty of mixing of the reactants, a single phase reaction is proposed (Boocock et al., 1998).*Corresponding author. E-mail: Tel: +234(803) The proposed model involves a cyclic solvent introduced361 1734 into the reaction mixture which makes both the oil and
  • 2. Mohammed-Dabo et al. 43methanol miscible by reduction of mass transfer Methodsresistance. This solvent has numerous numbers of Oil extractionsolvents with the boiling point up to 100°C (Caglar, 2007).Tetrahydrofuran (THF) (65.8°C) is preferred because of The Jatropha seed was weighed, grinded and the chaff separatedits close boiling point to that of methanol (64.4°C) so that from the kernel and both were weighed. Then the kernel wasafter reaction, both methanol and THF is recycled in a grinded and steamed in an oven to reduce the viscosity of the oilsingle step to be used again. The addition of THF to after which a mechanical extractor was used to extract the oil fromcreate a single phase greatly accelerates the reaction so the cake. Respective weights of the cake and the extracted oil were measured.that 99.89 wt%, whose conversion is almost complete, isachieved in a very short reaction time, such as 10 min(Boocock et al., 1998). The primary concerns with Oil characterizationcosolvent transesterification are the additional complexityof recovering and recycling the cosolvent, although this The oil was characterized for physical and chemical properties such as viscosity, FFA content, acid, saponification, iodine and calorificcan be simplified by choosing a cosolvent with a boiling values. Others are density and moisture content.point near that of the alcohol being used (Caglar, 2007).Additional concerns have been raised about the hazardlevel associated with the cosolvents. Several cosolvent Viscosity determinationare considered to replace THF among which are ethylacetate, diethyl ether, and 1,4-dioxane (Boocock et The viscosity of the raw oil was measured using Brookfield rotary digital viscometer NDJ-8S at 24.3°C. 200 ml of the oil was pouredal.,1998) each offering a unique set of properties and into a beaker and spindle, No 2 was attached to the viscometer, thisadvantages. was then lowered into the beaker and allowed to attain same This transesterification process is associated with many temperature with the sample and viscometer was set at a speed ofprincipal problems of which the reactants (oils and 60 rpm. While the viscometer was on, the reading at 25% shearalcohols) are not readily miscible because of their rate was taken.chemical structures. Oil disperses in the methanolmedium, so the probability and the rate of collision of the Free fatty acid determinationglyceride and the methoxide (the mixture of methanol andthe alkaline catalyst – KOH or NaOH) molecules This is the percentage by weight of specified fatty acid in the oil.becomes slower. This lowers the rate of collisions of The method applied for this analysis, is the American Oil Chemistsmolecules and also the rate of reaction causing longer Society (AOCS) method 5a-40. 1 g of sample was measured in a conical flask and dissolve with 25 ml of isopropyl alcohol. 3 drops ofreaction times, higher operating expenses and labour, phenolphthalein indicator was added to the solution. The mixturehigher fixed capital investments and consequently higher was then titrated with 0.1 N sodium hydroxide solution shakenproduct costs (Caglar, 2007; Behzadi and Mohammed, constantly until a pink colour persisted for 30 s. The percentage2007). FFA was then calculated using the formula: Many researchers have investigated the cosolventtransesterication of various edible vegetable oils,establishing various optimum operating conditions for (1)those oils (Antoline et al., 2002). Out of the availableresearches, none has neither critically used J. curcas oil Acid value determination(which non-edible) for the cosolvent transesterification This is the number of milligram of KOH required to neutralize thenor establish the process optimum parameters. This work free fatty acid in 1 g of the sample. 1 g of sample was weighed intotherefore seeks to cosolvently transesterify Nigerian J. a conical flask, 25 ml of the sample was poured into the conicalcurcas seed oil, employing tetrahydrofuran as the flask and 3 drops of phenolphthalein was added and titrated againstcosolvent. Establishing the optimum transesterification 0.1 N solution of potassium hydroxide. The acid value wasconditions was equally an objective this research work calculated according to the following formula:was set to achieve. (2)MATERIALS AND METHODSMaterials Saponification value determinationDried J. curcas seeds were obtained from Oil Seed Research unit This is the milligram of KOH required to saponify 1 g of fat or oil.of the Institute for Agricultural Research (IAR), Ahmadu Bello Saponification value is the measure of the molecular weight of theUniversity Zaria. Tetrahydrofuran (THF), anhydrous methanol, fatty acid. The AOCS method Cd 3-25 was employed. 2 g of thesodium hydroxide, tetraoxosulphate (IV) acid, hydrochloric acid, sample was weighed into a 250 ml conical flask and 50 cm 3 of 0.5carbon tetrachloride, potassium iodide, potassium dichromate and N ethanolic KOH (that has stayed overnight) was added to theWijs solution were procured from Chemical Stores in Zaria, Nigeria. sample. The mixture was then heated to saponify the oil. TheAll the procured chemicals were of analytical grades. unreacted KOH was then back titrated with 0.5 N hydrochloric acid
  • 3. 44 J. Pet. Technol. Altern. Fuels Stirrer Thermometer 3-Necked flask Bath Heat source Figure 1. Esterification/Transeterification experimental set up.using 2 to 3 drops of phenolphthalein indicator. The saponification drying method. The oil was heated at 130°C for 1 h and filteredvalue was calculated using the formula: using muslin cloth to drive off the water and remove the solid particles respectively. (3) Oil pre-treatment The oil extracted contain water and some solid particle, it wasIodine value determination heated at a temperature of 130°C for 30 min to boil out the water (Singh, 2009), it was then allowed to cool and settle over night, andThis is the measure of the degree of unsaturation in relation to the further, filtered with fine filter mesh to remove the solid particles.amount of fat or oil. Iodine value is defined as the gram of iodine The removal of water from the oil is necessary because waterabsorbed per 100 g sample. When unsaturated oil is heated, content of above 0.5% facilitate saponification.polymerization of the triglyceride occurs which leads to gumformation. Also, unsaturated compounds are susceptible tooxidation when exposed to air, thereby degrading the oil quality.Hence, the higher the iodine value, the greater the degree of Oil esterificationunsaturation. The method employed was AOCS method 1b-87. 2 g The oil had an FFA content of 14.8%, and therefore, there is needof the sample weighed into a 250 ml conical flask, 10 cm 3 of CCl4 for reduction below 0.5%, otherwise there will be high saponificationwas then added to dissolve the sample by swirling, 20 cm3 of Wij’s (Van Gerpen, 2005). This reduction was achieved via esterificationsolution was added and stoppered immediately, then swirled and of the oil with methanol and using tetraoxosulphate (VI) acid as thethe mixture was allowed to stand in the dark at ambient catalyst. 50 g of the oil was measured and place into three necktemperature for 30 min. 15 cm3 of 10% KI solution was then added round bottom flask and placed in a water bath and heated to awith 100 cm3 of distilled water to rinse the flask and the solution was temperature of 60°C. 5% w/w acid was mixed with 20% w/wthen titrated with a solution of sodium thiosulphate using starch methanol and also heated to a temperature of 60°C and mixed withindicator. A blank sample was prepared and back titrated the oil. A suspended mechanical stirrer was inserted into the oil viaaccordingly. The iodine value was calculated using the formula: one of the necks, the flask was equipped with a reflux condenser and a thermometer was dipped into the mixture via the remaining neck of the flask. The mechanical stirrer was set at 700 rpm and (4) timing was started at this point. A picking pippeted was used to withdraw samples at one hour interval (1, 2, 3, 4 and 5 h) and was titrated against 0.1 N solution of KOH to determine the %FFA level.Specific gravity determination The experimental setup is shown in Figure 1.A clean dried density bottle of 25 ml capacity was weighed (Wo), itwas then filled with the oil, stopper was inserted and reweighed Oil transesterification(W1), the oil was then substituted with water and weighed. Thespecific gravity was calculated using the following formula: The esterified oil was transesterified in 50 g batches to establish the optimum conditions for the reaction by varying the time at 10, 20, 30, 40, 50 and 60 min, and the temperature at 30, 40, 50 and 60°C. (5) The methanol to oil molar ratio and the Methanol-to-Cosolvent (THF) volume ratio were varied at 3:1, 4:1, 5:1, 6:1 and 1:1, 1:2, 1:3 respectively. The effect of stirring speed was also investigated byMoisture content determination varying it at 100, 200, 300, 400, 500, 600 and 700 rpm. The transestrification was carried out in the same set-up used forThe moisture content of the raw oil was also determined using oven esterification (Figure 1).
  • 4. Mohammed-Dabo et al. 45 Separating funnel Biodiesel layer Glycerol layer Figure 2. Separation set up. Table 1. Fatty acid composition of the raw J. curcas oil. S/No. Component Composition (Wt %) Molecular weight 1 Palmitic acid (16:0) 15.86 256.42 2 Linoleic acid (18:2) 37.24 280.45 3 Oleic acid (18:1) 37.13 282.46 4 Stearic acid (18:0) 9.76 284.48 Total 99.99 Average molecular weight (g/mol) 1103.81 Table 2. Properties of the raw J. curcas oil. S/No. Property Unit Value 1 FFA % 14.8 2 Saponification value mg KOH/g oil 202.34 3 Iodine value g of Iodine/100g of sample 100.56 4 Cetane number - 50.65 5 Density Kg/m3 874 6 Calorific value MJ/Kg 81.90 7 Viscosity at 25°C mPa.s 151.4 8 Acid value % 29.6 9 Moisture content % 0.4Ester purification produced had comparable properties with ASTM D 6751-02 standard B100.In each case the mixture was neutralized by addition of 1 drop of0.6 N H2SO4 cooled in an ice bath and poured into a separatingfunnel to separate the fatty acid methyl ester (FAME) from theglycerol by gravity. The experimental setup is shown in Figure 2. RESULTS AND DISCUSSIONThe glycerol, which settled at the bottom, was drained off while themethyl ester was washed with hot distilled water and dried. Characterization of the raw J. curcas oilEster characterization Tables 1 and 2 respectively present the compositional analysis and properties of the raw J. curcas oil. It can beUpon establishing the optimum conditions, the oil produced at theoptimum conditions was characterized for fatty acid methyl ester observed from Table 1 that the oil consisted principally ofusing GC-MS and other properties were also measured in 15.86, 37.24, 37.13 and 9.76% w/w palmitic, linoleic,accordance with the standard methods to see if the biodiesel oleic and stearic acids respectively. The fatty acid
  • 5. 46 J. Pet. Technol. Altern. Fuels Table 3. Results of esterification. S/No. Time (min) FFA (%) 1 0 14.8 2 60 8.23 3 120 6.55 4 180 5.43 5 240 2.55 6 300 0.4composition of the crude J. curcas seed oil used in this Optimizing the transesterification processwork is comparable to those reported by Makkar et al.(1997). This indicates that the oil contained more Having reduced the FFA of the raw oil, transesterifactionunsaturated fatty acids (linoleic acid and oleic acid) than process was carried out on the oil with a view tothe saturated fatty acids (palmitic acid and stearic acid). establishing the optimum operating conditions for theThe oxidative stability of biodiesel is a function of the fatty biodiesel production. The variables optimized includedacid composition of the parent oil. The higher the amount reaction time, temperature and agitation. Others are theof saturated fatty acid in the parent oil the greater the methanol-to-oil ratio, methanol-to-cosolvent ration andoxidative stability of the oil and vice versa. the catalyst (NaOH) concentration. It should be noted that Properties of the raw J. curcas oil presented in Table 2 in this research work THF was chosen as the cosolvent.were found to be within the literature values (Alptekin andCanakci, 2008). These include; saponification value(202.34 mgKOH/g oil), iodine value (100.56 g of Effect of reaction timeiodine/100g of oil), cetane number (50.6484), density(874Kg/m3), viscosity (151.4 mPa.s at 25°C) andmoisture content (0.4%). The calorific value of the raw J. Duration of reaction has been established as one of thecurcas oil was found to be 37.23 MJ/Kg. However, the critical parameters for biodiesel production. However, itfree fatty acid content of the raw Jatropha oil was found has been found out that incorporation of a cosolvent toto be 14.8% which was not within the ASTM specified the transesterfication alcohol leads to the reduction of thelimit of ≤0.5% for biodiesel production. Therefore the raw reaction time. To investigate the effect of time on theJ. curcas oil needs to be neutralized, through process, batches of 50 g of the esterified oil wereesterification. transesterified with a methanol/oil ratio of 3:1, catalyst (NaOH) concentration of 0.5% w/w of oil, 30°C reaction temperature and methanol-to-cosolvent ratio of 1:1% v/v at stirrer speed of 100 rpm. The reaction time was variedResults of estrification at 10, 20, 30, 40, 50 and 60 min. At these conditions, the highest yield of 73.5% was obtained at the 50 minAs stated previously, the free fatty acid content of the raw reaction time. However, as can be observed from FigureJ. curcas oil was not within the specified ASTM standard 3, at the first 10 min, about 73% yield of biodiesel wasfor biodiesel production; therefore, there was the need to obtained. Ideally, when optimizing a process, a point withneutralize the FFA through esterification by reacting the the highest yield is usually considered as the optimumoil with the methanol in the presence of tetraoxosulphate but here, considering the fact that the difference between(IV) acid. Table 3 shows the obtained esterification the yield at 10 and 50 min was just 0.5%, 10 min wasresults at various reaction times ranging from 0 to 300 chosen as the optimum reaction time. This is in order tomin. This was done with the view of reducing the oil’s save cost of heating that would be required to heat theFFA content to enable us carry out the transesterification vessel for 50 min just to attain an extra 0.5% yield of theon the oil. It can be observed from the Table 3 that at fatty acid methyl ester (FAME).zero minute, the FFA content of the oil was 14.8%. Thisvalue decreased to 8.23% after the first 60 min of thereaction, 6.55% after 120 min of the reaction and 5.43% Effect of reaction temperatureat 180 min of the reaction, this further dropped down to2.55% at 240 min before it finally came down to 0.4% Temperature is one of the significant factors affectingafter 300 min of reaction, which is within the specified biodiesel yield. Reaction temperature must be lower thanlimit of ≤0.5% for transesterification process (Singh, the boiling point of the alcohol in order to ensure that the2009). alcohol will not leak out through vaporization. Having
  • 6. Mohammed-Dabo et al. 47 Yield (%) Time (min) Figure 3. Effect of reaction time on the biodiesel yield. Yield (%) Temperature (°C) Figure 4. Effect of reaction tempearture on the biodiesel yield.established 10 min as the reaction time, the oil was significantly affect the yield of biodiesel. Figure 5 showstransesterified at the earlier stated condition for 10 min the effect of Methanol-to-oil ratio on the fame yield. It canunder various temperatures of 30, 40, 50 and 60°C. vividly be noticed that biodiesel yield is increased whenFigure 4 illustrates the effect of reaction tempearture on methanol to-oil-ratio is raised beyond 3:1 and reaches athe biodiesel yield. maximum. Increasing the alcohol-to-oil ratio beyond the As can be observed from figure, the highest yield of optimum did not increase the yield; instead it will increase81% was obtained at a reaction temperature of 40°C. the cost of recovery of the methanol and causes difficultyBeyond this temperature, the yield decreased drastically. in glycerol separation consequently resulting in lowerThe decrease in yield at temperature above 40°C could yield. When the Methanol-to-oil ratio was varied at 3:1,be as result of saponification reaction noticed at tempe- 4:1, 5:1 and 6:1 the highest biodiesel yield 98% wasrature above 40°C. Therefore, the optimum temperature obtained at 4:1 ratio. Further increase in the ratio resultedis 40°C as oppose to the 60°C reported by Demirbas into decrease in the yield. Therefore, the optimum(2009) for conventional transestrification (without a methanol-to-oil ratio was chosen as 4:1. It should becosolvent) noted that, this transesterification stage was conducted at 40°C, methanol-to-cosolvent ratio of 1:1% v/v, stirrer speed of 100 rpm, and catalyst concentration of 0.5%Effect of methanol-to-oil ratio w/w of oil for 10 min.Even though theoretically (from the transesterificationreaction stoichiometry), methanol-to-oil ratio of 3:1 is Effect of catalyst concentrationrequired for transestrification reaction. However,researches have indicated that methanol-to-oil ratio Investigating the effect of catalyst concentration (NaOH)
  • 7. 48 J. Pet. Technol. Altern. Fuels Yield (%) Methanol- to-oil ratio (% w/w) Figure 5. Effect of methanol-to-oil ratio on the biodiesel yield. Yield (%) Catalyst concentration (% w/w) Figure 6. Effect of catalyst (NaOH) concentration on the biodiesel yield.on the yield of biodiesel was carried out by varying the transfer resistance (Encinar et al., 2010). At this stage ofconcentration of NaOH at 0.5, 1.0, 1.5 and 2.0% w/w of the work, methanol-to-cosolvent (Tetrahydofuran) ratiooil and keeping the other variables stated above was varied at 1:1, 1:2 and 1:3% v/v while keeping otherconstant. The result shown in Figure 6 indicates that the reaction variables constant. Figure 7 presents theoptimum catalyst concentration was 0.5% w/w. Further influence of methano-to-cosolvent ratio on the biodieselincrease in concentration of catalyst beyond this yield. The figure indicates that for this investigation, thefacilitated saponification reaction and caused difficulty in optimum methanol-to-cosolvent volume ratio is 1:1 whichthe biodiesel separation from glycerol (Shay, 1993). This gives a yield of 98%. Further increase in the ratio resultedresulted in lowering the yield of the biodiesel at higher in the decrease of the biodiesel yield. This could probablycatalyst concentration. This finding corroborates with the be as a result of the dilution effect on the reagents.findings of Encinar et al. (2010) that the introduction of acosolvent to the transesterification alcohol reduces theamount of catalyst required. Effect of agitation In conventional transestrification reaction, agitation is aEffect of methanol/cosolvent volume ratio significant factor affecting yield of biodiesel. Several works have been conducted to investigate this effect,As opposed to conventional transestrification cosolvent Vincent (2005) and Antoline et al. (2002) reported 600transestrification offers significant reduction in mass rev/min as the optimum impeller speed. The effect of
  • 8. Mohammed-Dabo et al. 49 Yield (%) Methanol-to-cosolvent ratio (% w/w) Figure 7. Effect of methano-to-cosolvent ratio on the biodiesel yield. Yield (%) Speed (rpm) Figure 8. Effect of agitation on the biodiesel yield.stirrer speed on the yield of biodiesel was investigated by 100 to 200 rpm especially for the first few minutes of thevarying the speed between 100 and 700 rev/min. Figure reaction could be sufficient.8 shows effect of agitation on the J. curcas biodieselyield. It can be observed from the figure that there is nodefinite trend. However, the highest yield value of 98.04% Characterization of the produced J. curcas biodieselwas obtained both at 200 and 600 rpm. Since actuallymixing is only needed to establish one phase, once this is Sample of the biodiesel produced at the optimumestablished, there is no need for agitation. In cosolvent conditions established previously was characterized totransestrification, cosolvent contributes to overcome ascertain its composition and relevant properties. Table 4region of slow rate and therefore agitation becomes presents the composition of the FAME produced from theinsignificant. In this case however, the optimum agitation J. curcas oil as extracted from the obtained various peaksmay be considered as 200 rev/min based on the highest of the GC-MS used. It can be noticed from the table thatFAME yields obtained at this condition. However, it the produced biodiesel consisted principally of the fattyshould be noted that the difference in biodiesel yield acid methyl esters of palmitic, linoleic, oleic and stearicbetween 100 rpm (98.0076%) and 200 rpm (98.0426%) acids, hence confirming a high quality product. It canwas just 0.035%. So based on the results of this equally be observed that traces of other methyl estersinvestigation, agitation of the reaction mixture for about were also observed in the composition of the produced
  • 9. 50 J. Pet. Technol. Altern. Fuels Table 4. Peak report of FAME produced at the optimum conditions. Peak number %area Component 1 0.17 Myristic acid, methyl ester 2 2.83 Palmitoleic acid, methyl ester 3 20.01 Palmitic acid, methyl ester 4 0.18 Cyclopropaneoctanoic acid, methyl ester 5 0.35 Margaric acid, methyl ester 6 44.95 Linoleic acid, methyl ester 7 17.86 Oleic acid, methyl ester 8 11.51 Stearic acid, methyl ester 9 0.72 Ricinoleic, methyl ester 10 0.79 Arachidic, methyl ester 11 0.24 Bet-monolinolein 12 0.08 Stearic acid diglycerin ester 13 0.12 Docosanoic acid, methyl ester 14 0.18 Lignoceric acid, methyl ester Total 100.00 FAME Table 5. Properties of biodiesel produced at the optimum conditions. S/No. Property FAME ASTM D6751-02 Petrodiesel 1 Cetane number 51.43 47 min 46 2 acid number, mg KOH/g 0.75 0.80 max 0.35 3 Total glycerol, % w/w 0.0 0.24 NIL 4 Water content, % v/v 0.0 0.05 0.02 5 Density, Kg/m3 869 875-900 850 6 Calorific value, MJ/Kg 38.53 - 42 7 Viscosity at 40°C, mm2/sec 4.6 1.9-6.0 2.6 8 Saponification value, mg KOH/g oil 200.28 - NIL 9 Iodine number, g /100g oil 103.2 - -biodiesesl. These traces could not affect the quality oleic acid, linoleic acid and stearic acid. The unsaturatedproperties of the fuel as indicated in Table 5. fatty acids were in higher quantity than the saturated acid The produced biodiesel at the optimum conditions was and therefore the oil is good for biodiesel production.analysed to ascertain its quality with respect to the 2. Properties of the crude J. curcus seed oil such asstandard biodiesel and petrodiesel properties. Table 5 viscosity, saponification value, Iodine value, cetaneshows the comparative properties of the produced J. number, calorific value, flash point etc., were found tocurcas oil biodiesel with respect to the ASTM biodiesl and have comparable values with those obtained in thepetrodiesel. It can be observed from the table that the literature with the exception of the % FFAproduced biodiesel (FAME) virtually conforms to the 3. The transesterification optimum conditions were foundproperties specified by the American standard (ASTM to be 40°C, 200 rpm, 0.5% w/w catalyst concentration,D6751-02) and most of the properties tally with those of 4:1 methanol-to-oil molar ratio, 1:1 methanol-to-cosolventthe conventional diesel oil (petrodiesel). The produced oil volume ratio and time of 10 min.can therefore conveniently be used in a diesel engine. 4. Transesterification proceeds to completion at an even lower impeller stirring speed of 200 rpm as compared to 600 rpm reported for conventional transesterification.CONCLUSIONS 5. Overall, the cosolvent transesterification offers an avenue for reduction in cost of material (in terms ofThe following conclusions were drawn from this research catalyst concentration) and energy (in terms of stirringwork: speed) in biodiesel production as well as significant1. The raw Jatropha seed oil was found to contain reduction in time of reaction for a possible continuesbasically four major fatty acids namely: palmitic acid, process of biodiesel production.
  • 10. Mohammed-Dabo et al. 516. The biodiesel produced was found to have properties Encinar JM, Gonzalez JF, Pardal H, Martinez GM (2010). Transestrification of rapeseed oil with methanol in the presence ofthat are within the ASTM standard for biodiesel and various co-solvents. Proceedings of the Third Internationalhave small of the cosolvent used. Symposium on Energy from Biomass and Waste. Venice, Italy, Nov., 8-11. Makkar HPS, Aderibigbe AO, Becker K (1997). ComparativeREFERENCES evaluation of non-toxic varieties of Jatropha curcas. J. Food Chem., 62(2): 202 – 218.Alptekin E, Canakci M (2008). Characterization of the key fuel Meda CS, Venkata RM, Mallikarjunand MV, Vijaya KR (2009). properties of methyl ester-diesels. Fuel, 88(1): 75-80. Production of Biodiesel from Neem Oil. Int. J. Eng. Studies, 1(4):Antoline G, Tinaut FV, Briceno Y, Castano V, Perez C. and Ramirez 295–302. AI (2002). Optimization of biodiesel production by sunflower oil Shay EG (1993). Diesel fuel from vegetable oils: Status and estrification. Bioresour. Technol., 83(2): 111-114. Opportunities. Biomass Bioenergy, 4:227-42.ASTM D 6751-02 (2008). Biodiesel standard. United State of America Van GJ, Gerhard K, Jurgen K (2005). Handbook of Biodiesel, AOCS Biodiesel National Board, November 2008. Press Champaign Illinois, 2005Behzadi S, Mohammed MF (2007). Production of Biodiesel Using a Vicent G, Martinez M, Aracil J, Esteban A (2005). Kinetics of Continuous Gas-Liquid Reactor, Department of Chemical and sunflower oil methanolysis. Ind. Engine. Chem. Res., 44(15): 5447- Materials Engineering University of Auckland, Auckland New 5454. Zealand. Available at: World Energy Outlook (2009). Reference Scenario, IEA/OECD. biodiesel-using-a-continuous-gas-liquid-reactor.pdfBoocock DGB, Samir KK, VM, Lee C, Buligan S (1998). Fast Formation of High Purity Methyl Esters from Vegetable Oils. J. Am. Oil Chem. Soc. (JAOCS), 75(9): 1167- 1172.Caglar E (2007). Biodiesel production using co-solvent. European Congress of Chemical Engineering. Copenhagen: Izmir Institute of Technology.Demirbas A (2009). Progress and recent trends in biodiesel fuels. Elsevier J. Energy Conversion Manage., 50 (2009) 14-34.