Assessment of process variables on the use of macauba pulp oil as feedstock for the continuous production of ethyl esters under pressurized conditions

ABSTRACT

This study evaluated the potential of macauba pulp oil (MPO) as a feedstock for continuous ester production using ethanol under pressurized conditions. Experiments were performed in order to obtain data for the effect of process variables on ethyl ester (FAEE) and free fatty acid (FFA) conversion in a catalyst-free process. From the results, it appears that the MPO to ethanol mass ratio and the pressure were the variables with more favorable effect on the evaluated response variables. The addition of n-hexane caused an increase in the production of esters; however, this had a negative effect on FFA conversion. The addition of water was unfavorable for oil processing with high acidity. In this process, esterification and transesterification occur simultaneously, and the high FFA content in MPO provides high yields (85 wt% of esters; 93% FFA conversion) at low temperature, since the esterification reaction rate is higher than the transesterification. The decomposition of fatty acids was evaluated and levels <5% were observed under the evaluated experimental conditions.

Keywords:
Acrocomia aculeata; continuous; catalyst-free; ethanol

INTRODUCTION

Currently, soybean is the main raw material for biodiesel production in Brazil, accounting for ~70% of national production, followed by beef tallow and cottonseed oil (ANP, 2014). However, the country has a large territory and climatic diversity, which gives great potential for production of cheaper raw materials (Silva and Freitas, 2008). The highest percentage of biodiesel production costs is caused by the price of the feedstock used (Robles-Medina et al., 2009), so the search for raw materials with low cost has become a key point towards economic competitiveness of this biofuel (Michelin et al. 2015).

Thus, other sources have been studied and can be used to obtain this biofuel. Among these is the fruit of macauba (Acrocomia aculeata), which stands out for its high yield potential because it can produce 4500 to 6000 liters of oil per hectare year (Bergmann et al., 2013; César et al., 2015), greater than the oil yield per hectare year of annual crops such as soybeans (560 liters), sunflower (774 liters) and castor (810 liters) (Bergmann et al., 2013). Ilha et al. (2014) showed that the biodiesel obtained from Acrocomia aculeata has acceptable properties for use in diesel engines; however, due to the predominant composition of unsaturated fatty acids, it requires the use of an antioxidant additive. Macauba oil is obtained from the pulp and almond, wherein the pulp comprises ~45% of the fruit (Ramos et al., 2008) and has between 18.7 to 29 wt% of oil (Coimbra and Jorge, 2012; Ciconini et al., 2013). The literature reports the high FFA content in macauba pulp oil (Doná et al., 2013; Aguieiras et al., 2014; Iha et al., 2014; Navarro-Díaz et al., 2014; César et al., 2015), between 10.5 to 65.4 wt%, due to the presence of fatty acids in the fruit tissues of Acrocomia aculeate (César et al., 2015) and because the oil is obtained by pressing and filtration without refining steps. The processing of this crude oil for biodiesel production requires the use of methods tolerant to free fatty acids (César et al., 2015).

Ilha et al. (2014) obtained macauba biodiesel using a two-step reaction: esterification of FFA with sulfuric acid and transesterification with potassium hydroxide. The use of the homogeneous catalysts requires the use of subsequent washing steps for removal of the catalyst from the product and thus leads to the generation of a high volume of effluents (Vyas et al., 2010).

Aguieiras et al. (2014) proposed the application of enzymatic hydroesterification of macauba oil (10.5 wt% of FFA) with yields of 85% in esters; however, long reaction times were applied at each step: 6 hours for hydrolysis and 4 hours for esterification. The alcoholysis of macauba oil (88.9 mg KOH g^-1 oil) in a process assisted by ultrasound is presented in the work of Michelin et al. (2015) using the commercial enzyme Novozym 435 as catalyst. In that study, the authors reported an ester yield of 75% at 60 minutes using 20% enzyme (by weight of the substrates), and reusing the enzyme was shown to be attractive for only five cycles. The results of Aguieiras et al. (2014) and Michelin et al. (2015) demonstrate the limitations of the enzyme-catalyzed method related to long reaction times or the need for high enzyme concentrations to reach satisfactory yields, which increases the process cost due to the high cost of the enzyme (Silva and Oliveira, 2014).

Aiming to solve the drawbacks of processes using homogeneous catalysts and enzymes, non-catalytic reactions in pressurized medium using alcohols at sub- or supercritical conditions can be applied, as it allows for the simultaneous transesterification of triacylglycerides and esterification of free fatty acids, and hydrolysis of triacylglycerides when water is present in the reaction medium (Warabi et al., 2004, Kusdiana and Saka, 2004). The fact that the alcohol is present under pressurized conditions in the reaction medium leads to higher solubility of the substrate, increasing reaction rates and ester yields (Silva and Oliveira, 2014). The use of this technique for MPO processing was reported by Navarro-Díaz et al. (2014) using ethanol and methanol in supercritical conditions; however, the FFA conversion under different reaction conditions was not reported. This was also seen in the work by Doná et al. (2013) for obtaining macauba biodiesel from interesterification with methyl acetate in supercritical conditions. The esterification reaction rate is faster than transesterification, and higher conversion of FFA can be obtained in subcritical conditions, as reported in the works of Vieitez et al. (2012) and Abdala et al. (2014a). Thus, since the MPO has high FFA levels, evaluation of the experimental conditions to allow the use of alcohol in subcritical conditions in the process has become a focus of study, and was not evaluated in the work by Navarro-Díaz et al. (2014).

Another difference in this study is related to the addition of co-solvent in the process, which may decrease the operational parameters such as temperature, pressure and the amount of alcohol (Muppaneni et al., 2012; Tan et al., 2010) as a result of the increasing mutual solubility between the oil and the alcohol (Abdala et al., 2014b). The use of n-hexane as co-solvent is effective in non-catalytic reactions, as can be seen in previous studies by our research group on the synthesis of ethyl esters from Jatropha oil (Silva et al., 2014) and used frying oil (Abdala et al., 2014b).

Based on the above, this work aimed to report experimental data on the reaction of macauba pulp oil with ethanol under pressurized conditions. The Plackett Burman (PB-12) experimental design was applied to assess the effects of process variables on ester yield and FFA conversion, and select the variables with the greatest influence on the reaction in pressurized conditions. The reactions were conducted under different operating conditions that made possible the use of ethanol as a sub- and supercritical fluid.

MATERIALS AND METHODS

Macauba pulp oil (Cocal - Brasil), ethanol (JT Baker 99.8%) and n-hexane (Vetec 98.5%) were used for the reaction without further treatment. Table 1 shows the fatty acid composition of the oil determined by gas chromatography using the procedure described by Navarro-Díaz et al. (2014). The oil has a FFA content of 70.26±0.05 wt% and water content of 0.76±0.001 wt%. For analysis of the reaction products, standard analytical methyl heptadecanoate (Sigma Aldrich, 99.9%), heptane (FMaia, 95%), ethanol (FMaia, 95%), ethyl ether (Nuclear), phenolphthalein (Nuclear), sodium hydroxide (Anidrol) and boron trifluoride-methanol (Sigma Aldrich) were used.

Table 1
Fatty acid composition of MPO.

Fatty acid	Content (wt%)
Capric	0.14 ± 0.01
Lauric	1.42 ± 0.08
Myristic	0.45 ± 0.01
Palmitic	13.54 ± 0.14
Palmitoleic	1.38 ±0.01
Stearic	3.87 ± 0.03
Oleic	69.95 ± 0.18
Linoleic	7.82 ± 0.12
Linolenic	0.52 ± 0.02
Eicosanoic	0.26 ± 0.01

The reactions were conducted in duplicate using a laboratory scale unit and the experimental procedure presented elsewhere (Doná et al., 2013). The specifications of the tubular reactor used are presented in detail in the work of Abdala et al. (2014b). The experimental procedure basically consists of pumping the reaction mixture to the reactor, preheated at the reaction temperature, until the time needed to fill the reactor and pressurization system.

After the steady-state condition was reached, i.e., after a reactor space-time had elapsed at least two times, samples were collected and stored for later analysis. A Plackett and Burman experimental design with 12 assays (PB-12) was employed to evaluate the effects of five variables, keeping the residence time fixed at 25 min. This methodology of screening design aims to select variables with the greatest influence on a certain response variable of interest (Rodrigues and Iemma, 2005). Residence time was defined as the time the mixed reactants remained in the tubular reactor, which equals the void volume of the reactor divided by the volumetric flow rate. Table 2 presents the process variables (design factors) and ranges investigated for the experimental designs used in this work. The MPO to ethanol mass ratios considered in Table 2, 1:0.5, 1:1.25 and 1:2, represent approximately 1:10, 1:15 and 1:20 MPO to ethanol molar ratios, respectively. The software Statistica® 7.0 (Statsoft Inc., USA) was used to assist the design and statistical analysis of the results, considering a significance level of 95%.

Table 2
Factors and levels investigated in the experimental design employed in this work in the simultaneous transesterification and esterification of macauba pulp oil (residence time fixed at 25 min).

Variable		Level
	-1	0	1
Temperature (K), T	523	548	573
Pressure (MPa), P	10	15	20
Mass ratio (MPO: ethanol), MR	1:0.5	1:1.25	1:2
Water addition (wt%), W	0	5	10
Cosolvent addition (wt%), CS	0	10	20

The procedure reported by Silva et al. (2010) was utilized for the analysis of ethyl esters and decomposition. The samples were injected, in triplicate, in the gas chromatograph (Agilent GC 7890), equipped with flame ionization detector and a capillary column (ZB-WAX, 30 m x 0.25 mm x 0.1 μm). The quantification of the ester content in the samples followed the standard UNE-EN 14103 method (2003) and the FAEE yield was then calculated based on the content of ethyl esters in the analyzed sample. To calculate the degree of decomposition, the equation proposed by Vieitez et al. (2008) was used. The term "decomposition" of fatty acids referred to the decrease in their percentages (determined by gas chromatography) due to the formation of other compounds, such as oxygenated compounds (Lee et al., 2012) and hydrocarbons (Shin et al., 2011).

The FFA content was determined by the Ca 5a-40 method (AOCS, 1998) and FFA conversion was calculated based on the content of free fatty acids in the oil and in samples of the reaction medium, as reported by Abdala et al. (2014a).

RESULTS AND DISCUSSION

Table 3 presents the matrix of the Plackett and Burman design with 12 assays (PB-12), with coded values for the independent (factors) variables: temperature, pressure, MPO to ethanol mass ratio, water and co-solvent addition, with the response in terms of FAEE yield and FFA conversion. The effects of the process variables on the simultaneous esterification and transesterification of MPO under pressurized conditions are presented in Table 4.

Table 3
Matrix of the PB-12 experimental design (coded values) with answers in terms of FAEE yield and FFA conversion (residence time fixed at 25 min).

Run	Variable/level						Answers
	Ta	Pa	MRa	Wa	CSa		FAEE yield (%)	FFA conversion (%)
1	1	-1	1	-1	-1		72.37±0.31	91.74±0.66
2	1	1	-1	1	-1		72.13±0.22	92.97±0.57
3	-1	1	1	-1	1		85.38±0.19	93.95±0.72
4	1	-1	1	1	-1		82.47±0.42	86.71±0.35
5	1	1	-1	1	1		77.77±0.37	69.18±0.46
6	1	1	1	-1	1		84.65±0.28	90.28±0.57
7	-1	1	1	1	-1		85.20±0.33	82.89±0.36
8	-1	-1	1	1	1		70.31±0.47	84.49±0.29
9	-1	-1	-1	1	1		76.94±0.54	65.58±0.33
10	1	-1	-1	-1	1		82.09±0.62	81.00±0.41
11	-1	1	-1	-1	-1		73.02±0.34	83.87±0.39
12	-1	-1	-1	-1	-1		73.82±0.42	84.25±0.44
13-15	0	0	0	0	0		72.55±0.36b	87.70±0.49b

• ^{a b}
  See Table 2; average of three experiments.

Table 4
Effect of independent variables on the simultaneous transesterification and esterification of macauba pulp oil.

	FAEE yield (%)			FFA conversion (%)
Variable	Effect	p-levela		Effect	p-levela
Mean/Intercept	76.92	<0.001		84.66	<0.001
Temperature	1.13	0.033		2.80	0.010
Pressure	3.35	0.003		3.22	0.007
MPO to ethanol mass ratio	4.10	0.002		8.86	0.001
Water addition	-1.08	0.036		-7.21	0.001
Cosolvent addition	3.02	0.004		-6.32	0.002

• ^a
  statistical significance p<0.05.

Effect of MPO to ethanol mass ratio

It can be seen in Table 4 that the MPO:ethanol mass ratio was the variable with the greatest significance in terms of ester yield and FFA conversion. Ester production may be favored by reaction displacement to the formation of products by increasing the alcohol to oil ratio beyond the stoichiometric value. In addition, an increase in ratio of ethanol to oil provided increased contact area between the reagents (Kusdiana and Saka, 2001) and decreased the critical temperature of the reaction mixture (Yujaroen et al., 2009; Olivares-Carrillo et al., 2014).

Samniang et al. (2014) reported the effect of the oil to ethanol molar ratio on the ester yield obtained from Krating oil (with an acid value of 29 mg KOH g^-1); using ratios of 1:20 and 1:40, 76.5 and 84.6 wt% esters was obtained, respectively, for reactions carried out at 533 K, 5 minutes and 16 MPa. Similar results were observed in the work of Gonzalez et al. (2013), where the yield of the reaction between ethanol and waste frying oil increased from 49.9 to 64.7% at 1:20 and 1:40, respectively, for reactions conducted at 573 K and 20 MPa.

An increase in the methanol:oil mass ratio from 0.5:1 to 1:1 favors the conversion of oleic acid at 583 K and 25 MPa, as shown by Ding et al. (2011). The same effect was observed in a study by Jin et al. (2015) by varying the methanol:oleic acid molar ratio from 1:1 to 20:1 at 533 K.

Effect of Pressure

From Table 4, it appears that an increase of pressure from 10 to 20 MPa caused an increase in the production of esters; however, the effect on the ester yield was more pronounced, considering the yield of esterification and transesterification reactions, than the FFA conversion. The solubility of free fatty acids at sub- or supercritical fluid conditions is greater than that of triacylglycerols, so the esterification reaction can proceed more easily (Warabi et al., 2004). Increased pressure favors the solubility of ethanol in oil. Accordingly, at higher pressures, the ethanol and oil form a more homogeneous mixture, thus facilitating the reaction.

An increase in pressure from 15 to 20 MPa favored obtaining esters of Jatropha oil at 573 K, with oil:ethanol mass ratio of 1:1 and 28 min, as shown by Silva et al. (2014). Under these conditions, the authors reported an increase in esters from 42 to 60 wt%. In the transesterification of macauba oil, with high acidity, Navarro-Díaz et al. (2014) reported an increase in the yield of ethyl esters from 43.1 to 53.3 wt% after increasing the pressure from 10 to 20 MPa at 573 K and 1:20 oil to ethanol molar ratio.

The work of Abdala et al. (2014a) reported that an increase in pressure from 15 to 20 MPa favors the conversion of oleic acid in ethanol for reaction times of 20 to 30 min using 1:6 oleic acid to ethanol molar ratio and temperatures of 523 and 528 K. Another study of interest is that of Wang et al. (2008), who investigated the effect of pressure on the reaction of soybean oil and a mixture of soybean oil+oleic or stearic acid with supercritical methanol and reported an increase in yield after increasing the pressure from 9 to 15 MPa.

Effect of Temperature

The alcoholysis reaction under pressurized conditions requires the application of high temperature conditions to obtain alcohol at sub- or supercritical conditions. In the reaction of MPO with ethanol, the temperature proved to be favorable in both reactions in the range of 523 to 573 K, as seen in Table 4. A temperature increase at higher pressures led to better miscibility between the triacylglycerols and alcohol (Tang et al., 2006), obtaining the supercritical phase for the triolein-ethanol system above 543 K at 200 bar and triolein:ethanol molar ratio of 1:42 (Almagrbi et al., 2012).

From the results in Table 3, it can be seen that high ester yields (>85 wt%) were obtained in the lower temperature reactions (runs 3 and 7). Esterification is a one-step reaction that can make it easier for the reaction to reach completion, whereas transesterification consists of three consecutive and reversible reactions. Thus, the effect of increasing the temperature under pressurized conditions is more pronounced for transesterification than for esterification, and it is possible to obtain high yields at low temperatures by increasing the FFA content in the oil.

In the transesterification of refined palm oil, Ngamprasertsith et al. (2014) showed an increase in the ethyl esters content from 45 to 72% upon increasing the temperature from 543 to 573 K at 20 MPa and 1:30 oil:ethanol molar ratio. Another interesting study was presented by Farobie and Matsumura (2015) for ethyl transesterification of canola oil; these authors reported increased ester yield of 17 to 38 wt% when the reaction temperature increased from 543 to 573 K at 20 MPa, for 15 minutes and oil to ethanol molar ratio of 1:40.

In the case of esterification, a temperature increase from 523 to 563 K caused an increase in the oleic acid conversion from 80 to ~93%, as can be seen in the results published by Ding et al. (2011) for reactions conducted at 25 minutes, with oleic acid:methanol mass ratio of 1:1 and 25 MPa. Abdala et al. (2014a) reported high conversion of oleic acid, i.e. 70%, in the reaction with ethanol at 20 MPa, with 1:1 oleic acid to ethanol mass ratio and 10 minutes at 473 K; this conversion increased to 88% at 573 K.

Effect of Cosolvent Addition

In an attempt to improve the reaction efficiency, n-hexane was added to the reaction mixture in proportions of 10 and 20 wt% (relative to oil). It was verified from the results (Table 4) that the transesterification reaction was favored, since the cosolvent increased the mutual solubility between ethanol and oil, thus reducing mass transfer limitations and increasing the reaction rates (Muppaneni et al., 2012; Silva et al., 2014). Using heptane as the cosolvent, Tan et al. (2010) reported a decrease in the optimum reaction temperature from 633 to 553 K with a cosolvent to methanol molar ratio of 0.15.

The use of n-hexane had a favorable effect on the increased production of esters for different reaction systems (Patil et al., 2010; Muppanemi et al., 2012; Abdala et al., 2014b; Silva et al., 2014). In this regard, we can cite the work developed by Patil et al. (2010), which evaluated the addition of n-hexane in the methyl transesterification of camelina oil at 563 K, with 1:25 oil:methanol molar ratio, 114 bar and 40 min of reaction. The ester yield increased from 46.6% to 88% with the addition of 20% (by volume of oil) of the cosolvent. Muppaneni et al (2012) report that, with the addition of 10% cosolvent (by volume of oil), the yield of esters increases from 45 to 70% at 568 K, 1:25 oil to methanol molar ratio, 110 bar and 20 min of reaction. The addition of a cosolvent was also effective in the transesterification of used frying oil as the ester yield increased from 34 wt% without a cosolvent, to 72 wt% with the addition of 20 wt% of n-hexane, at 573 K, oil:ethanol mass ratio of 1:1, 20 MPa and 40 min (Abdala et al., 2014b).

Regarding the esterification, the addition of a solvent has a negative effect on FFA conversion. Imahara et al. (2009) reports that the addition of n-hexane can dilute the reactants, thus decreasing the reaction rate. The authors also mention that this effect is more pronounced at elevated temperatures, explaining the low FFA conversion obtained at 573 K with 20% of cosolvent (runs 5 and 9).

Whereas the transesterification reaction has lower reaction rates and required higher temperature conditions to provide high yields of esters, when compared to esterification, the overall assessment of the cosolvent effect is that it is favorable for obtaining esters of macauba pulp oil, with high acidity, using pressurized ethanol.

Effect of Water Addition

Water addition to the reaction medium was found to be unfavorable for the production of esters from MPO under our experimental condition. The presence of water causes the production of FFA by the hydrolysis of triacylglycerols (Kusdiana and Saka, 2004) and can also cause hydrolysis of the esters formed during the reaction (Yujaroen et al., 2009; Ding et al., 2011; Go et al., 2014).

The work of Navarro-Díaz et al. (2014), relating to the reaction of macauba oil with high acidity, i.e. 56.3 wt% FFA, shows that the addition of water to a level of 10 wt% (to ethanol) at 573 K, 20 MPa and oil:ethanol molar ratio of 1:40 reduced the yield of ethyl esters, compared to the reaction without water, for all residence times considered under these conditions. Similar observations were reported by Yujaroen et al. (2009) upon the addition of 5 to 30% (v/v) in the esterification of a palm fatty acid distillate using supercritical methanol. The authors also evaluated the hydrolysis of esters at different reaction times and found than 573 K and 25 min led to the hydrolysis of ~20% of methyl esters.

Comparison with the literature

Based on the effects observed for each variable, the highest ester yield (85.38 wt%) was obtained at 523 K, 20 MPa, and MPO:ethanol mass ratio of 1:2, without water and 20 wt% of the cosolvent. The high FFA content of MPO provides a high yield of esters in ethanol subcritical conditions due to the high conversion of FFA, i.e. 93.95%, under these conditions. This result is greater than the highest yield, 69.6 %, reported by Navarro-Diaz et al. (2014) at 598 K, 15 MPa, oil:ethanol molar ratio of 1:30, 5 wt% water added to the ethanol and 35 minutes of reaction, obtained at low temperature.

Table 5 shows a comparison of the results obtained in this work with recent data published in the literature for reactions using ethanol under pressurized conditions. From the data in this table, it appears that the high amount of FFA in macauba oil might act as a catalyst to accelerate the reaction to produce more esters. This fact, coupled with the use of co-solvent in the process, provided high ester yields at low reaction temperature and short reaction time when compared to other studies.

Table 5
Comparison of the results obtained in this work with the literature using ethanol in pressurized conditions.

Oil; acidity	Conditions	FAEE (wt%)	Reference
Macauba pulp oil; 70.25 wt% of FFA	1:2 oil to ethanol mass ratio (~1:20 oil to ethanol molar ratio); 523 K; 20 MPa; 25 minutes and 20 w% of cosolvent addition	85.38	This Work
Waste fried oil; 1.5 wt% of FFA	1:30 oil to ethanol molar ratio; 598 K; 15 MPa; ~46 minutes and 5 w% of water addition	82.2	Gonzalez et al. (2013)
Castor oil; 1.4 wt% of FFA	1:40 oil to ethanol molar ratio; 623 K; 14.5 MPa; 10 minutes	56.17	Rodríguez-Guerrero et al. (2013)
Waste fried oil; 3.73 mg KOH.g-1	1:20 oil to ethanol molar ratio; 573 K; 20 MPa; 70 minutes and 20 w% of cosolvent addition	~87	Abdala et al. (2014b)
Used palm olein oil; 11.1 mg KOH.g-1	1:30 oil to ethanol molar ratio; 573 K; 30 MPa; ~40 minutes	70	Ngamprasertsith et al. (2014)
Macauba pulp oil; 56.3 wt% of FFA	1:30 oil to ethanol molar ratio, 598 K, 15 MPa, 35 minutes and 5 wt% of water addition	69.6	Navarro-Diaz et al. (2014)
Jatropha oil; 10.1 wt% of FFA	1:20 oil to ethanol molar ratio; 573 K; 20 MPa; 52 minutes	80	Silva et al. (2014)
Camelina oil; 1.7 wt% of FFA	1:40 oil to ethanol molar ratio; 583 K; 20 MPa; 30 minutes	86	Sun et al. (2014)
Canola oil; not reported	1:40 oil to ethanol molar ratio; 573 K; 3.54 MPa; 25 minutes	~60	Farobie and Matsumura (2015)

Decomposition of Fatty Acids

Figure 1 illustrates the decomposition of fatty acids for the experimental runs shown in Table 3. It can be seen from the results in Figure 1 that up to 5% decomposition was observed under all evaluated conditions. The highest levels of decomposition were observed for reactions conducted at 573 K (runs 5 and 6), followed by the midpoint of the conditions at 548 K (runs 13 to 15). For experiments conducted at 523K (runs 8, 9, 11 and 12), low values (<0.2%) for decomposition of fatty acids were observed. Analysis of these data shows the high influence of temperature on the decomposition of fatty acids, as already reported by Silva et al. (2010), Vieitez et al. (2012) and Silva et al. (2014). The best ester yield was observed at a temperature of 523 K (run 3) and in this condition ~1% decomposition was reported, consistent with the results of Vieitez et al. (2010), who reported on the high stability of ethyl esters at this temperature.

Figure 1
Decomposition of fatty acid from the conditions of Table 3.

For the studied system (macauba pulp oil/ethanol) and evaluated experimental range a direct correlation between decomposition and the variables considered in Table 2 was not observed, probably because of the low decomposition levels observed. These low levels of decomposition may be related to the high content of free fatty acids in the oil, since Vieitez et al. (2012) reported that increasing the acidity of the oil reduced decomposition. The authors reported that this effect may have been due to the lower availability of glycerol in the reaction medium, which decreases the occurrence of side reactions between this byproduct and other components of the reaction medium.

CONCLUSIONS

In this work, the continuous and non-catalytic reaction of macauba pulp oil (MPO) with ethanol under pressurized conditions was studied to assess the operational variables in the use of this feedstock for biodiesel production. The variable MPO:ethanol mass ratio had the greatest influence on the evaluated reaction parameters, followed by pressure and temperature. The production of esters was favored by the addition of n-hexane in the reaction medium. The possible hydrolysis of esters upon the addition of water was unfavorable in this system. The reaction of MPO with high acidity using a cosolvent in the reaction mixture can be conducted at low temperatures in high yields (85 wt% of esters, 93% conversion of FFA) and low levels of decomposition (~1%).

ACKNOWLEDGEMENT

The authors thank CNPq and Fundação Araucária for the financial support and West Paraná State University (UNIOESTE) for the scholarship.

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Publication Dates

• Publication in this collection
  July 2017

History

• Received
  26 Apr 2016
• Accepted
  02 June 2016