G. simplicifolia seeds served as plant materials for GSO extraction. The climbing shrub has orbicular and glabrous-shaped seeds in kidney-shaped pods (Figure 1(a)). At maturity, the pods split open, allowing for the collection of mature seeds from the floor. The seeds (Figure 1(b)) were harvested near the botanical garden of the Faculty of Sciences at the University of Lomé from December 2019 to March 2020. Afterward, the seeds were sun-dried, dehulled (Figure 1(c)), and grounded (grain diameter ≤ 2 mm).

In addition, crude palm kernel oil (PKO) served as a secondary raw material to compensate for the insufficient amount of G. simplicifolia seed oil that we extracted. The choice of PKO supplied by a cooperative was motivated by its abundance and affordability in the local markets in Togo. The optimal temperature and reaction time obtained during the transesterification of PKO were assumed to be identical for GSO conversion.

The Soxhlet extraction of G. simplicifolia seed oil with hexane was performed four times using m_o = 250 g of seeds powder at each run. After 6 h, the solvent was evaporated using a Büchi rotary evaporator with the heating bath B-100 set at 40˚C. Some residual hexane was definitively removed from the recovered oil fraction through oven-drying at 80˚C for 2 h. The resulting oil was stored at −40˚C for further use. The oil extraction yield, denoted as Y (%), was calculated using Formula (1).

Y ( % ) = mass ( flask + oil ) − mass ( flask ) massofseedspowder × 100 (1)

In the first step, the palm kernel oil (PKO) was settled down to decant, and the supernatant was removed and dehydrated using anhydrous Na₂SO₄. Subsequently, the resulting product was oven-dried at 105˚C ± 2˚C for 2 h before being hot-filtered. The recovered PKO was considered ready to transesterify and was stored at −40˚C for further use.

The triglycerides in PKO and GSO were reacted with methanol under base-cat- alyzed conditions using NaOH or KOH. The reaction vessel temperature was regulated using a TERMAKS/Model B 2324 V incubator system (T_max = 64˚C), and permanent mixing was achieved using a magnetic stirrer (VWR model 320) with a rotation speed set at 300 rpm. A thermometer was used to ensure the proper temperature of the pre-heated oil before adding the catalytic mixture (MeOH + NaOH or KOH).

After the reaction, the resulting mixture was transferred to a separating funnel. After 60 minutes, two immiscible phases were formed in the separating funnel. Then, the lower phase, mainly composed of glycerol, excess catalyst, altered pigments, etc. was separated from the FAME phase. Subsequently, the FAME phase was washed in multiple runs with near-boiling distilled water (water volume = 1/3 volume of the FAME phase). A colorless washing effluent upon adding phenolphthalein indicated a catalyst-free FAME mixture. The purification step of the previous FAME mixture involved residual methanol and free water removal by evaporating at 103 ± 2˚C for 20 minutes, dehydration with Na₂SO₄, and hot-filtration.

The one-factor-at-a-time method was adopted for optimizing the PKO-to-me- thanol (PKO/MeOH) molar ratio, the reaction time, and the reaction temperature. The experimental conditions are presented in Tables 1-3, respectively.

The optimal GSO-to-MeOH molar ratio and the influence of the catalyst type (NaOH or KOH) were investigated. The tested molar ratios were 1:6, 1:9, and 1:12. For each run, the mass of GSO used was 20 g; the required weights of NaOH

Constants: mass of PKO = 20 g; temperature T = 60˚C, reaction time t = 100 min and catalyst amount = 1.95% NaOH (w/w).

Constants: Mass of PKO = 20 g; PKO/MeOH molar ratio = 1:12; Temperature T = 60˚C and catalyst amount = 1.95% NaOH (w/w).

Constants: Mass of PKO = 20 g, PKO/MeOH molar ratio = 1:12; reaction time t = 60 min; catalyst amount = 1.95% NaOH (w/w).

or KOH catalysts were calculated using Formula (11) and Formula (12), respectively. The reaction temperature and time were identical to their optimal values determined for PKO, therefore set at T = 63.5˚C and t = 60 min, respectively.

The qualitative monitoring of FAME formation has been performed by measuring changes in density and refractive index as a function of the kinetic parameters mentioned earlier, in reference to previous works by Froehner et al. (2007) [21] and De Filippis et al. (1995) [22] .

Assuming that each triglyceride was converted into methylesters, some fuel properties of G. simplicifolia biodiesel, namely: the cetane number (CN), the kinematic viscosity (ν), the higher heating value (HHV), the volumetric energy density, the oxidative stability (OSI), and the cloud point (CP) were predicted exploiting GSO fatty acids composition and using identical mathematical models as those suggested by Talebi et al. (2014) [23] in their online graphical user interface BiodieselAnalyzer 2.2.

Each value in this study was presented as the mean of the measurements from two trials plus the standard deviation of the mean. The line plots were generated using Python 3 Matplotlib library. For comparison of the catalytic effect of NaOH or KOH, a multiple t-test was performed using GRAPHPAD 8.4.3. If p-value > 0.01, the difference was considered non-significant, and significant otherwise.

G. simplicifolia seed oil and palm kernel oil physicochemical parameters are summarized in Table 4.

GSO extraction yield

The extraction yield of G. simplicifolia seed oil was 28.06% ± 0.38%. This yield was similar to the average values reported by Novidzro et al. (2019a) [11] and Giurleo (2017) [29] , respectively 28.40% and 27% - 32%. Compared to soybean bearing an oil content ranging between 18% - 21% [30] , G. simplicifolia seeds with an estimated oil content of 30.72% (Novidzro et al., 2019a) [11] showcase an attractive oleaginous potential to be valorized in downstream processes to 5-HTP extraction. Therefore, botanical studies are needed to harness the reproduction of the plant. Besides, technical and economic analyses are required to assess the profitability of such processes.

Refractive index

The refractive index ( n D 20 ) measured for was 1.4651 ± 0.0001. This value was lower than 1.4715 ± 0.0011 found by Novidzro et al. (2019a) [11] in a previous

^aIV: determined experimentally using Wijs method; ^bIV: predicted exploiting GSO fatty acids profile (Formula (4)); ^aSV détermined experimentally using volumetric titration; ^bSV: predicted exploiting GSO fatty acids profile (Formula (3)); ND: Non-Determined; NA: Non-applicable.

study. It is frequently verified that ( n D 20 ) increases with the degree of unsaturation and the length of fatty acids lateral chain. In this study, the simultaneous effect of the higher concentration of C18 fatty acids and the higher degree of unsaturation (152%) of our GSO compared with that of Novidzro et al. (2019a) [11] would imply a higher ( n D 20 ) for our GSO. Such discrepancy means that other factors such as the unsaponifiable fraction would have much more influence on ( n D 20 ).

Specific gravity

The specific gravity at 15˚C of the extracted GSO calculated using the equation of Lund gave 0.92368, corresponding to a density at 15˚C of 0.92287 g/mL. This density exceeded the maximum range recommended for biodiesel, which is 0.860 g/mL to 0.900 g/mL [31] . This result indicated that neat GSO must be transesterified prior to possible usage in diesel engines.

Higher heating value

The estimated HHV for GSO was 39.57 MJ/kg. This value was in the same range as those reported in the literature for regular feedstocks used in biodiesel production, such as castor oil (39.79 MJ/kg), soybean oil (39.64 MJ/kg), sunflower seed oil (39.59 MJ/kg), and linseed oil (39.34 MJ/kg) [19] .

Acid value and concentration of free fatty acids

Using volumetric titration, GSO and PKO acid values were 2.86 ± 0.00 mg KOH/g and 18.01 ± 0.08 mg KOH/g, respectively. These values corresponded to free fatty acid percentages of 1.43% (w/w) and 6.43% (w/w), respectively. For GSO, the obtained value was below the tolerable threshold of 2.5% (w/w) indicated by Musa (2016) [32] as safe for alkaline homogeneous transesterification. However, this acidity was higher than the 0.5 (% w/w) value mentioned by Freedman et al. (1984) [33] for achieving maximum methylesters yield (>98%). But, with preliminary dehydration, indirect heating, and moderate stirring rate, side reactions like saponification are less likely to occur. In the case of PKO, due to its high free fatty acids content, species presenting surfactant behavior are more likely to form during its conversion into biodiesel. Therefore, heterogeneous acid catalysis would be the preferred method of conversion.

Saponification value

The determined SV for our GSO, 172.59 ± 1.32 mg KOH/g was lower than the 186.59 ± 0.63 mg KOH/g previously obtained by Novidzro et al. (2019a) [11] . This difference is due to the higher C18 fatty acids content in our GSO (92.21%) compared to 87.88% from Novidzro et al. (2019a) [11] study. This difference also resulted in an approximate ten-unit difference in molecular weight. As for PKO, the obtained SV of 221.17 ± 0.14 mg KOH/g was below the range of 240 mg KOH/g - 257 mg KOH/g reported by some authors for palm kernel oils [34] . With respect to the latter, the transesterification of PKO would result in a lower methylesters yield compared to GSO, because the higher the SV of the oil, the lower methyl esters yield is obtained after base-catalyzed transesterification. Furthermore, additional precautions should be taken during the washing step of PKO biodiesel, because this type of oil tends to easily give tensioactive molecules in alkaline conditions, which will act as emulsion stabilizers, thus hindering the aqueous and organic phase proper separation.

Ester percent

The ester percent is a metric for evaluating the quality of a raw material that will undergo homogeneous base-catalyzed transesterification. In this study, EP values of 98.34% ± 0.02% and 91.86% ± 0.02% were determined for GSO and PKO, respectively. Referring to the previous values, only GSO could provide a FAME yield greater than 98%, as Canesin et al. (2014) [17] reported a minimum of 96.5% glycerides to achieve a yield greater than 98%.

Iodine value

The experimental IV of our GSO was 25.58 ± 0.32 g I₂/100g of oil. This result was in a similar range as the IVs of palm kernel oils from the literature (15 - 23 g I₂/100g) and consistent with the previous determination by Novidzro (2019a) [11] classifying GSO as a non-drying oil. However, the theoretically calculated IV and DU based on GC-MS data were 132.23 g I₂/100g and 152.07%, respectively. The previous demonstrated considerable difference between theoretical and experimental values. The theoretical IV appeared more plausible considering the total amount of unsaturated fatty acids (UFA) in GSO, namely 79.50%. Additionally, the DU of our GSO, 152.07, was quite comparable to that of other oils with a similar unsaturated fatty acids composition, such as sunflower oil and soybean oil, which have DU values of 152.2% and 143.8%, respectively, with respective IVs of 132 g I₂/100g and 128 g I₂/100g [18] . If the theoretical result were given superior credit, it would imply that GSO is a drying oil since its IV is greater than 110 g I₂/100g. In the latter scenario, the IV of GSO significantly exceeded the maximum value (IVmax = 120 g I₂/100g) recommended by the European standard EN-14214 for feedstocks suitable for biodiesel production [35] . Furthermore, the theoretical degree of unsaturation of GSO surpassed the threshold indicated in European specifications, DUmax = 137 [18] . Finally, further investigation is required to explain conclusively the substantial gap between the experimental and theoretical results.

The GC-MS analysis of the fatty acids composition of GSO provided the results summarized in Table 5. As per analysis results, GSO presents a high level of linoleic acid of 72.56%. The latter content was similar to the 73.19% reported by Novidzro et al. (2019c) [36] . Moreover, the aggregate percentage of unsaturated fatty acids (UFA), including linoleic acid (72.56%), oleic acid (6.93%), palmitoleic acid (0.01%), and (Z)-hexadec-11-enoic acid (0.01%) in our GSO, was 79.51%.

Other vegetable oils, such as safflower oil and grape seed oil, also shows similar linoleic acid percentage [37] . In the present GSO, palmitic and stearic acids were the predominant saturated fatty acids, with 7.54% and 12.72%, respectively.

¹ND: Non-Determined, ²MUFA: Monounsaturated Fatty Acid, ³PUFA: Polyunsaturated Fatty Acid.

The previous palmitic and stearic acids contents in our GSO were in equal range as the values reported by other authors, ca. 9% - 11% for C16:0 and 16% - 18% for C18:0 [38] and 8.8%, 16.9% for C16:0 and C18:0, respectively [29] . The high cumulative amount of C18 fatty acids in GSO, ca. 92.21%, would favorably influence the cetane number (CN), as CN tends to increase when the aliphatic lateral chain length of fatty acids approach or exceed that of n-hexadecane. Conversely, the high content of unsaturated fatty acids (UFA), with a total amount of 79.51%, would adversely affect CN value, as CN decreases when the degree of unsaturation (DU) increases [39] . Moreover, the high UFA content is beneficial for the viscosity, as the latter tends to decrease with the increasing DU of the oil [40] . Similarly, the relatively low content of saturated fatty acids (SFA) in our GSO (20.42%) should result in more advantageous cold flow properties.

In this study, we qualitatively accessed the yield of FAME after each PKO sample transesterification experiments by measuring the variation in density and refractive index of the resulting transesterified mixtures. The data points obtained allowed the construction of the line plots depicted in Figures 2(a)-(c).

It is worth mentioning that the density values used to establish the line plots were measured without accounting the effect of air buoyancy. Therefore, in this section the density implies non-corrected density ρ_nc.

With respect to the FFA content of the PKO used in this study (6.43%), the optimal reaction conditions for the transesterification reaction, were: optimal

reaction temperature T_opt = 63.5˚C, optimal reaction time t_opt = 60 min, and optimal PKO/MeOH molar ratio MR_opt = (1:12). Following each experiment, a diminution in the value of the density of the formed FAME mixtures compared to the parent oil was observed versus increasing reaction parameters values, either PKO/MeOH molar ratio (Figure 2(a)) or reaction time (Figure 2(b)) or reaction temperature (Figure 2(c)). The density ρ_nc decreased from the maximum value of 0.8942 g/mL (neat PKO) to a minimum of 0.8401 g/mL as PKO/MeOH molar ratio increased from (1:3) to (1:12). Beyond a molar ratio exceeding MR = 1:12, the opposite effect occurred. In particular, at MR = 1:3, the obtained reaction mixture solidified in the separating funnel. Such an observation is due to the higher rate of the saponification reaction of glycerides compared to that of the transesterification reaction.

The reduced density of the transesterified product compared to that of the parent oil is due to the progressive substitution of the glycerol moiety in glycerides by methanol molecules. Since pure glycerol is denser than neat vegetable oil, its cleavage out of the medium consequently leads to a decrease in the density of the resulting mixture. However, an excessive excess of methanol resulted in poor separation of the FAME phase from the glycerol phase leading to a decrease in FAME yield. The presence of diluted glycerol in the FAME phase leads to the apparent loss of methyl esters due to micelles formation [32] . Additional explanation suggested by Phan & Phan (2008) [41] assumed a reduction in the rate of conversion of triglycerides into FAMEs. According to the latter hypothesis, one must first consider the mechanism through which excess methanol would initially lead to a high conversion of glycerides into FAME. Afterward, as more FAME molecules are formed, consequently increasing amount of glycerol is generated. Ultimately, as the reaction medium approaches saturation in glycerol, the excess glycerol molecules in the medium would automatically shift the equilibrium to the reverse side in compliance with the laws of thermodynamic equilibria.

The line plots obtained by measuring the density and refractive index of transesterified mixtures at selected molar ratios depending on the catalyst type (NaOH or KOH) are depicted in Figure 3, Figure 4 and Table 6. Regardless of catalyst type, GSO/PKO MR = 1:9 resulted in the FAME mixtures with optimal density and refractive index, thus predictively optimal FAME yield. Expectedly, the refractive index of the transesterified mixtures decreased as the oil-to-methanol molar increased (Figure 5 and Table 6). In other words, the refractive index of transesterified vegetable oils decreases as the FAME yield increases, in compliance with the results of Xie & Li (2006) [42] . Additionally, the paired-com- parison plots comparing KOH or NaOH capability in lowering the refractive index and the density of parent oils are illustrated in Figure 5 and Figure 6. According to the latter results, there was no significative differences in the catalytic

n D T : refractive index; ρ_nc: density.

performance of NaOH or KOH, either during GSO (p = 0.1449 > 0.05) or PKO (p = 0.5240 > 0.05) conversions. Many attempts at establishing a linear regression relationship between the refractive index and the yield of alkylesters as a rapid method of verification in continuous biodiesel production are available in the literature [43] [44] [45] .

Finally, in the present study the preferred optimal reaction conditions for the transesterification of GSO were as follows: 1.3% KOH (w/w); GSO/MeOH molar ratio MR_opt = 1:9; reaction time t_opt = 60 min, and temperature T_opt = 63.5˚C. There is however, a need of quantitative instrumental techniques such as Gas Chromatography (GC) or High-Performance Liquid Chromatography (HPLC) to measure the FAME yield and validate our assertions.

The physicochemical parameters of GSO biodiesel calculated using various linear regression correlations and relying upon data from the fatty acid composition of GSO are compiled in Table 7.

The calculated OSI of GSO biodiesel resulted in an induction period of 0.65 hours. This induction period did not comply with the EN 14214 (3 h) and ASTM 6751 (6 h) specifications. According to previous work by Kumar (2017) [46] , GSO biodiesel would be classified as a biodiesel with poor oxidative stability, since OSI < 2 h. Therefore, according to Kumar (2017) [46] , this type of biofuel would require a significant amount of antioxidant additives, regardless of specifications, to achieve the recommended quality, thus incurring higher costs. Being predominantly unsaturated (DU ≈ 152), the bis-allylic positions Δ11 of polyunsaturated fatty acids (PUFA) and allylic positions Δ11 of monounsaturated fatty acids (MUFA) will have a strong tendency to undergo homolytic cleavage under oxidative conditions. As a result, it is imperative to implement efficient storage conditions to isolate GSO and resulting biodiesel from ambient air, light, metals, or other pro-oxidative factors.

The higher heating value (HHV) calculated for GSO biodiesel was 39.72 MJ/kg. The latter value is approximately 8% lower than that of No. 2 petrodiesel fuel [47] . Correspondingly, the previous value relates to a volumetric energy density of 34.97 MJ/L, which is considerably lower than that of petrodiesel, ca. 40 MJ/L [48] . Consequently, a volume of ca. 1144 mL of GSO biodiesel would be required to deliver equal energy output as 1 L petrodiesel, thus negatively affecting the pump prices. Therefore, to maximize the energy return on investment (EROI), it will be best to align this process with the valorization of niche molecules such as 5-HTP, lectins, and antioxidants in G. simplicifolia seeds.

¹CN: Cetane Number; ²HHV: Higher Heating Value; ³CP: Cloud Point; ⁴ν: kinematic viscosity; ⁵OSI: Oxidative Stability Index.

The calculation of the cetane number (CN) of GSO biodiesel yielded 50.29. This value complies with ASTM D 6751 specification. Comparatively, the calculated CN value was close to those of soybean biodiesel (51.8) and sunflower biodiesel (51.9) [49] .

The determination of the kinematic viscosity at 40˚C of GSO biodiesel resulted in a value of 4.07 mm²/s. This value adhered to EN 14214 and ASTM D 6571 specifications. However, it significantly exceeded that of Ultra Low Sulfur Diesel, which is 2.32 mm²/s [50] .

The predictive calculation of the cloud point of GSO biodiesel using the correlation suggested by Sarin et al. (2009) [28] gives a value of −1.03˚C. Nonetheless, minor compounds in GSO, such as sterylglycosides, terpenoids, and phospholipids, can dramatically influence this parameter up. In reality, it is plausibly expectable that the experimental cloud point of GSO biodiesel might be higher than the theoretically predicted value depending on the presence and quantities of these minor compounds.

Apart from the poor oxidative stability (OS), each fuel property calculated in this study for GSO biodiesel complies with the European EN 14214 and the American ASTM D 6571 standards.