# Catalytic Activity of a Bifunctional Catalyst for Hydrotreatment ofJatropha curcas L. Seed Oil

Authors: J. García-Dávila; E. Ocaranza-Sanchez; C. Sánchez; A. L. Martínez-Ayala
Journal: Journal of Spectroscopy
 (2018)

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## Abstract

The hydrotreating process of vegetable oils (HPVO) involves the transformation of vegetable oil triglycerides into straight chain alkanes, which are carried out by deoxygenation reactions, generating multiple hydrocarbon compounds, cuts similar to heavy vacuum oil. The HPVO is applied toJatropha curcas oil on USY zeolite supported with gamma alumina and platinum deposition on the catalytic as hydrogenation component. The acid of additional activity of the supports allows the development of catalytic routes that the intervention of catalytic centers of different nature reaches the desired product. The products of the hydrotreating reaction with Jatropha curcas seed oil triglycerides were identified by Fourier transform infrared spectroscopy and by mass spectroscopy to identify and analyze the generated intermediate and final hydrocarbon compounds.


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## Body

## 1. Introduction

Currently, there is a decline in fossil fuel reserves by contrast, every year the increase in demand for liquid fuels, such as environmental pollution due to excessive use; it is necessary to obtain renewable liquid fuels from natural sources. Triglyceride-based vegetable oils are a potential raw material for the production of biofuels.Jatropha curcas seed oil is one of the most important alternative nonedible types of vegetable oils for biofuel production [1]. The fluid catalytic cracking (FCC) process uses fossil fuels to produce, that is, gasoline, diesel, and olefins, where large molecules are broken down with the help of a catalyst [2].Catalyst is the key factor in promoting high activity and selectivity to product distribution. In fact, new research materials focus on improving catalytic activity and generate fewer by-products and contaminants [3]. The heterogeneous catalyst is the great economic impact as the USY zeolite which provides high activity and selectivity of the catalysts. USY is a large pore crystalline material having a maximum aperture of 0.74 nm, a cell unit size of about 2.45 mm, a Si/Al ratio of 3 to 5, and having shape selectivity to have the sites more active in the microporous structure [4].The zeolite USY is widely used as a catalyst support and plays an important role in the catalysts used in the hydrocracking process because they enhance catalytic activity, selectivity, or stability imparting shape selectivity [5]. However, the high acidity of the zeolite carrier increases undesirable cracking activity, which accelerates the rate of coke deposition. The incorporation of a metallic phase on the support materials with a high dispersion allows the development of catalytic routes in which the intervention of catalytic centers of different nature achieves the desired product [6] (multifunctional catalysts).Conventional hydrotreating involves the removal of heteroatoms, such as sulfur and nitrogen. The hydrocracking process involves the saturation and breakage of C-C bonds to produce high-grade gasoline and diesel fuels [7]. A novel alternative for the production of biofuels is catalytic hydrotreatment and hydrocracking of vegetable oils [8].Hydrotreatment of vegetable oil and its mixtures with heavy vacuum gas oil has been explored to produce biofuels using conventional hydrotreating catalysts based on Ni-Mo/Al2O3 and Co-Mo/Al2O3 [9] under conventional conditions of nominal hydrodesulfurization operation [10]. A novel alternative to manufacture biofuels is catalytic hydrotreatment and hydrocracking of vegetable oils. Several hydrotreated vegetable oils include palm oil [11], Jatropha curcas L. [12], Jatropha cinerea oil [13], and soybean lecithin [14].USY zeolite has been reported to use as a catalyst for cracking of waste cooking oils [15] and Jatropha curcas [16]. Favor you apply in very different pressure and temperature conditions. In this work, we use the γ-alumina which is the most commonly used as support on which the active component in this case is dispersed the zeolite USY which presents activity acid. In addition, in the form of dispersion are incorporated platinum particles that act as a function of hydrogenation in the catalyst for the hydrotreatment of Jatropha curcas seed oil [17].


## 2. Experimental

### 2.1.Jatropha curcas Seed Oil

TheJatropha curcas L. seed species used in this study are native to the state of Puebla, Mexico. The seed oil was extracted by mechanical pressing using an ELVEC press. The vegetable oil was used without a pretreatment.


### 2.2. Preparation of Zeolite USY

The support used wasγ-alumina with a specific surface area of 270 m2/g and a volume of 0.8 cm3/g. It was mixed with zeolite USY at 10 and 20 wt%. The samples were extruded and dried at 110°C overnight and calcined in air at 500°C for 4 h. This mixture was used as platinum metal support. The catalysts were prepared by impregnating the aqueous solution of chloroplatinic acid (H2PtCl6) as a precursor using the incipient impregnation wetness method. After impregnation, the sample was dried at 110°C overnight, followed by calcination at 500°C for 4 h in a muffle furnace. After activation, the catalyst was reduced for 4 h at 400 psia and 400°C under a hydrogen flow of 60 mL min−1.The adsorption of water was used as a manual method for the determination of the specific surface [18]; it is a simple and economical approximation to obtain the value of 0.45 mL/g of catalyst (±0.01). Both the pore volume and the pore size of the zeolite are smaller than the alumina sample. The presence of Pt partially reduces the sites, responsible for coking [19] for their masking with the metal particles Pt; hence, the activity of the catalyst persists over a long period.


### 2.3. Catalytic Activity

The catalytic performance of the bifunctional catalyst was investigated by hydrotreatingJatropha curcas seed oil in a continuous flow tubular reactor of 9 mm internal diameter and 300 mm in length vertically within the tubular programmable temperature. Nitrogen gas was introduced into the system to fully purge air from the system while the reactor reached the desired temperature. The hydrotreating process was carried out under the following conditions: temperature 310, 360, and 390°C, total pressure 400 psi, hourly space velocity by weight (WHSV) 176.4–35.28 h−1 (0.5 and 0.1 g of the catalyst were charged), and hydrogen to feed oil molar ratio of 15.


### 2.4. Analysis of Hydrotreatment Samples

The analysis of the products was performed using a Fourier transform infrared spectroscopy (FTIR). Using a Bruker Vertex-70 unit in an ATR (attenuated total reflectance) sampling mode, the system is equipped with an OPUS program for data acquisition and the region of measurement was the middle infrared (4000–400 cm−1) with a resolution of 4 cm−1. Subsequently, the liquid products were analyzed using an Agilent 7890A GC/MSD gas chromatograph, with the G4513A auto sampler coupled to a 5975C VL MSD mass spectrometer with triple axis detector; a capillary HP-5MS (30 m∗320 μm∗0.25 μm) was used with the external standard technique for quantification. The GC/MSD parameters were oven program, 70°C for 5 min, 20°C/min at 200°C for 5 min, and then 10°C/min at 300°C for 5 min, with an injection volume of 2 μL and temperatures of 230°C and 150°C for MS source and quadruple, respectively, with the ChemStation program for data acquisition in mode scan.A calibration curve was taking from the previous work of García-Dávila et al. [20] that represents the band intensity quantification at 1743 cm−1 and 1160 cm−1, indicating the abundance of fatty acids (Figures 1 and 2). Using Jatropha curcas seed oil spectrum as the maximum content of oxygenates compounds, and n-hexadecane as hydrocarbon molecule model as the minimum oxygenated compounds, this compound was taken an internal standard to represent the final hydrotreatment product. The reduction of the signal in the band intensity at 1743 cm−1 and 1160 cm−1 was quantified and correlated with the conversion [21].Figure 1
FTIR spectra of calibration curve ofJatropha curcas oil with hexadecane [12].Figure 2
Calibration curve ofJatropha curcas seed oil dilutions with hexadecane at 1743 and 1160 cm−1 wavelength [12].


## 2.1.Jatropha curcas Seed Oil

TheJatropha curcas L. seed species used in this study are native to the state of Puebla, Mexico. The seed oil was extracted by mechanical pressing using an ELVEC press. The vegetable oil was used without a pretreatment.


## 2.2. Preparation of Zeolite USY

The support used wasγ-alumina with a specific surface area of 270 m2/g and a volume of 0.8 cm3/g. It was mixed with zeolite USY at 10 and 20 wt%. The samples were extruded and dried at 110°C overnight and calcined in air at 500°C for 4 h. This mixture was used as platinum metal support. The catalysts were prepared by impregnating the aqueous solution of chloroplatinic acid (H2PtCl6) as a precursor using the incipient impregnation wetness method. After impregnation, the sample was dried at 110°C overnight, followed by calcination at 500°C for 4 h in a muffle furnace. After activation, the catalyst was reduced for 4 h at 400 psia and 400°C under a hydrogen flow of 60 mL min−1.The adsorption of water was used as a manual method for the determination of the specific surface [18]; it is a simple and economical approximation to obtain the value of 0.45 mL/g of catalyst (±0.01). Both the pore volume and the pore size of the zeolite are smaller than the alumina sample. The presence of Pt partially reduces the sites, responsible for coking [19] for their masking with the metal particles Pt; hence, the activity of the catalyst persists over a long period.


## 2.3. Catalytic Activity

The catalytic performance of the bifunctional catalyst was investigated by hydrotreatingJatropha curcas seed oil in a continuous flow tubular reactor of 9 mm internal diameter and 300 mm in length vertically within the tubular programmable temperature. Nitrogen gas was introduced into the system to fully purge air from the system while the reactor reached the desired temperature. The hydrotreating process was carried out under the following conditions: temperature 310, 360, and 390°C, total pressure 400 psi, hourly space velocity by weight (WHSV) 176.4–35.28 h−1 (0.5 and 0.1 g of the catalyst were charged), and hydrogen to feed oil molar ratio of 15.


## 2.4. Analysis of Hydrotreatment Samples

The analysis of the products was performed using a Fourier transform infrared spectroscopy (FTIR). Using a Bruker Vertex-70 unit in an ATR (attenuated total reflectance) sampling mode, the system is equipped with an OPUS program for data acquisition and the region of measurement was the middle infrared (4000–400 cm−1) with a resolution of 4 cm−1. Subsequently, the liquid products were analyzed using an Agilent 7890A GC/MSD gas chromatograph, with the G4513A auto sampler coupled to a 5975C VL MSD mass spectrometer with triple axis detector; a capillary HP-5MS (30 m∗320 μm∗0.25 μm) was used with the external standard technique for quantification. The GC/MSD parameters were oven program, 70°C for 5 min, 20°C/min at 200°C for 5 min, and then 10°C/min at 300°C for 5 min, with an injection volume of 2 μL and temperatures of 230°C and 150°C for MS source and quadruple, respectively, with the ChemStation program for data acquisition in mode scan.A calibration curve was taking from the previous work of García-Dávila et al. [20] that represents the band intensity quantification at 1743 cm−1 and 1160 cm−1, indicating the abundance of fatty acids (Figures 1 and 2). Using Jatropha curcas seed oil spectrum as the maximum content of oxygenates compounds, and n-hexadecane as hydrocarbon molecule model as the minimum oxygenated compounds, this compound was taken an internal standard to represent the final hydrotreatment product. The reduction of the signal in the band intensity at 1743 cm−1 and 1160 cm−1 was quantified and correlated with the conversion [21].Figure 1
FTIR spectra of calibration curve ofJatropha curcas oil with hexadecane [12].Figure 2
Calibration curve ofJatropha curcas seed oil dilutions with hexadecane at 1743 and 1160 cm−1 wavelength [12].


## 3. Results

### 3.1. Spectrometry FTIR

The hydrotreatment tests were performed by testing the Al2O3 support loaded with two percentages of 10 and 20% USY zeolite to observe the effect of the acid activity of the zeolite on the oil. Subsequent to the appropriate relationship, platinum (Pt) molecules are incorporated by the incipient wetness impregnation method to add the hydrogenating function; two different weight fractions as indicated in Table 1 were tested to quantify the specific metallic activity in the catalyst.Table 1
Formulation of bifunctional catalyst for hydrotreatment ofJatropha curcas seed oil.
Quantity of USY zeolite on gamma alumina
Catalyst charging to the reactor (g)
Platinum (%)
0% USY/Al2O310% USY/Al2O320% USY/Al2O3
0.5
0.05
0.01
0.1
0.05
0.01A comparison of hydrotreated samples was carried out by attenuated total reflectance spectroscopy (FTIR-ATR), where the amplitude of the oil peaks was compared with the amplitude of the peaks of the hydrotreated samples. It was taken as the baseline below the n-hexadecane spectrum (100% conversion) andJatropha curcas oil as the upper base (0% conversion) to standardize the magnitudes of the FTIR peaks and quantitatively establish the conversion, a calibration curve by means of dilutions of the oil with hexadecane (Figures 1 and 2). From the correlation of the signal intensity of the spectra by the FTIR of the samples, the limit of the superior of the respect and the inferior one determined the progress in the reduction of the band intensity of the fatty acids in a process of hydrotreatment of Jatropha curcas seed oil.There was a decrease in the characteristic peaks of the fatty acids in the hydrotreatment samples; this phenomenon was registered at temperatures of 310°C according to the increase of the operating temperature. To discriminate the thermal cracking effect on the hydrotreatment process, a test without catalyst was run, where the evidence shows that there is no significant difference between the FTIR spectra with respect to the crude oil which demonstrates that there is no thermal degradation of the triglyceride and the process only develops as a function of the bifunctional catalyst (Figure3). These data are consistent with those reported by Idem et al. [22] for canola oil, wherein the thermal cracking is significant above 400°C and increases with operating temperature.Figure 3
FTIR spectra of hydrotreated oil at different temperatures with WHSV of 3 min−1 with 20% USY/Al2O3 without metallic active phase.It is observed that at higher USY zeolite/alumina ratio, there is a higher acid activity like sulfur-type catalysts such as Co-Mo and Ni-Mo, with conversions above 60% at residence times, like those reported for other catalysts [23].From the analysis by FTIR, a shift to low frequencies in the wave number is observed by the presence of characteristic peaks of carbonyl and carboxyl groups. These representing the formation of compounds with functional groups of ketones and aldehydes which are considered as the first intermediate products generated in the hydrotreatment process [24] after the disintegration of the triglyceride, this information will be corroborated by gas chromatography coupled to mass spectroscopy.The absorption band shift was recorded with a wavelength of 1743 to 1710 cm−1 corresponding to group (C = O) characteristic of ketones and aliphatic aldehydes Figure 4 unlike the group (C = O) of the fatty acids that has a lower stability because of not containing the (OH) group. The signal from this group increases its absorbance by increasing the operating temperature of the hydrotreatment process, which indicates that more fatty acid reduction is present at higher operating temperatures [25].Figure 4
Displacement of absorption bands in hydrotreated samples with 20% USY catalyst with WHSV of 35.28 h−1.With the formulation of the 20% USY/Al2O3 catalyst, platinum particles were incorporated by the incipient wetness impregnation method. To this end, a solution of chloroplatinic acid H2PtCl6 was prepared from the grams of platinum to be incorporated into the matrix of 0.01, 0.05, and 0.1 g, respectively, with a comparison being made between the catalytic activities for each formulation of the bifunctional catalyst.The results show that the catalyst with the highest activity to hydrocarbon transformation is the formulation with 20% of zeolite USY/Al2O3 with a percentage of 0.01% Pt (Figure 5). Since at higher percentages, the metallic phase does not allow the transition towards the acid phase, which results in a rapid saturation of the free fatty acids not allowing molecular cracking reactions [26]. The total triglyceride conversion is proportionality to temperature. At 310°C, conversion levels reach 20% with 0.01% Pt loaded; at 350°C, conversion levels increase until 40%; and finally at 390°C, conversion levels increase to 75% at WHSV 35.3 h−1.Figure 5
Comparative catalytic activity in samples hydrotreated by FTIR at different temperatures and WHSV with platinum-loaded 20% USY/Al2O3 catalyst. (black square) 0.01% Pt WHSV = 176.4 h−1; (light gray square) 0.01% Pt WHSV = 35.28 h−1; and (dark gray square) 0.05% Pt WHSV = 35.28 h−1.


### 3.2. CG/MSD

A comparative study of the degree of reaction progression by FTIR and CG/MSD was carried out, where it was observed (Figure6) that there is a higher degree of advancement by FTIR compared to CG/MSD for the same samples; with increasing temperature at 390°C, there is a significant difference between the yields for the same catalyst formulation.Figure 6
Comparative maximum conversion and hydrotreated samples by FTIR and CG/MSD at different temperatures with catalyst 0.01% Pt and 20% USY/Al2O3 at WHSV = 35.28 h−1.Despite this, both analytical techniques coincide in the formulation of the catalyst with 20% of zeolite USY/Al2O3 with a percentage of 0.01% Pt as the formulation of greater activity in the hydrotreatment process. The discrepancies in absorbance values obtained by FTIR are overestimated by the presence of compounds with similar C = O binding. This is attributed to the formation of light fatty acids of lower molecular weight compared to the initials present in the triglyceride. It is known that in the process, hydrotreating occurs first before hydrocracking [27]. Whereby at a temperature of 310°C, there is more hydrogenation/dehydrogenating activity than acidic activity [28].By FTIR analysis, the light fatty acids considered them as reactive for keeping the C=O bond current, while for CG/MSD, they were considered as reaction intermediates since they are not part of the initial triglyceride. This difference is observable for each operating temperature performed in this work, where there is the presence of other functional groups that makes the reaction follow-up similar by both techniques.The formation of partially deoxygenated groups increases as temperature and WHSV increase; these compounds are considered as primary intermediates of reaction of the free fatty acids to olefins and as by-products of reaction to the alkanes and aromatics as a result of processes of cyclization and hydrogenation of the olefins [29]. The hydrocarbon cuts formed have a high selectivity towards the formation of chains of the order of diesel and in less amount hydrocarbon formation of the order of jet fuel and gasolines in a proportion of 6 : 1 and 21 : 1, respectively, Figures 6, 7, and 8.Figure 7
Catalytic activity forJatropha curcas L. seed oil. Catalytic selectivity in functional groups for bifunctional catalyst 0.01% Pt and 20% USY/Al2O3 at WHSV = 35.28 h−1.Figure 8
Yield in hydrocarbon cuts as a function of temperature and WHSV with bifunctional catalyst 0.01% Pt and 20% USY/Al2O3.It is clearly observed that at a temperature of 390°C, there is a higher formation of hydrocarbons of the order of diesel with a yield of more than 35%, while for jet fuel and gasolines are maintained at yields of less than 10%; this emphasizes that the catalyst is selective to cuts of diesel. Similar results have been reported by Zheng et al. [16] and Li et al. [15] who reported similar conversions of 68.6% and 58.7% of liquid products, respectively, at higher WHSV and temperature values compared with those used in this research.


## 3.1. Spectrometry FTIR

The hydrotreatment tests were performed by testing the Al2O3 support loaded with two percentages of 10 and 20% USY zeolite to observe the effect of the acid activity of the zeolite on the oil. Subsequent to the appropriate relationship, platinum (Pt) molecules are incorporated by the incipient wetness impregnation method to add the hydrogenating function; two different weight fractions as indicated in Table 1 were tested to quantify the specific metallic activity in the catalyst.Table 1
Formulation of bifunctional catalyst for hydrotreatment ofJatropha curcas seed oil.
Quantity of USY zeolite on gamma alumina
Catalyst charging to the reactor (g)
Platinum (%)
0% USY/Al2O310% USY/Al2O320% USY/Al2O3
0.5
0.05
0.01
0.1
0.05
0.01A comparison of hydrotreated samples was carried out by attenuated total reflectance spectroscopy (FTIR-ATR), where the amplitude of the oil peaks was compared with the amplitude of the peaks of the hydrotreated samples. It was taken as the baseline below the n-hexadecane spectrum (100% conversion) andJatropha curcas oil as the upper base (0% conversion) to standardize the magnitudes of the FTIR peaks and quantitatively establish the conversion, a calibration curve by means of dilutions of the oil with hexadecane (Figures 1 and 2). From the correlation of the signal intensity of the spectra by the FTIR of the samples, the limit of the superior of the respect and the inferior one determined the progress in the reduction of the band intensity of the fatty acids in a process of hydrotreatment of Jatropha curcas seed oil.There was a decrease in the characteristic peaks of the fatty acids in the hydrotreatment samples; this phenomenon was registered at temperatures of 310°C according to the increase of the operating temperature. To discriminate the thermal cracking effect on the hydrotreatment process, a test without catalyst was run, where the evidence shows that there is no significant difference between the FTIR spectra with respect to the crude oil which demonstrates that there is no thermal degradation of the triglyceride and the process only develops as a function of the bifunctional catalyst (Figure3). These data are consistent with those reported by Idem et al. [22] for canola oil, wherein the thermal cracking is significant above 400°C and increases with operating temperature.Figure 3
FTIR spectra of hydrotreated oil at different temperatures with WHSV of 3 min−1 with 20% USY/Al2O3 without metallic active phase.It is observed that at higher USY zeolite/alumina ratio, there is a higher acid activity like sulfur-type catalysts such as Co-Mo and Ni-Mo, with conversions above 60% at residence times, like those reported for other catalysts [23].From the analysis by FTIR, a shift to low frequencies in the wave number is observed by the presence of characteristic peaks of carbonyl and carboxyl groups. These representing the formation of compounds with functional groups of ketones and aldehydes which are considered as the first intermediate products generated in the hydrotreatment process [24] after the disintegration of the triglyceride, this information will be corroborated by gas chromatography coupled to mass spectroscopy.The absorption band shift was recorded with a wavelength of 1743 to 1710 cm−1 corresponding to group (C = O) characteristic of ketones and aliphatic aldehydes Figure 4 unlike the group (C = O) of the fatty acids that has a lower stability because of not containing the (OH) group. The signal from this group increases its absorbance by increasing the operating temperature of the hydrotreatment process, which indicates that more fatty acid reduction is present at higher operating temperatures [25].Figure 4
Displacement of absorption bands in hydrotreated samples with 20% USY catalyst with WHSV of 35.28 h−1.With the formulation of the 20% USY/Al2O3 catalyst, platinum particles were incorporated by the incipient wetness impregnation method. To this end, a solution of chloroplatinic acid H2PtCl6 was prepared from the grams of platinum to be incorporated into the matrix of 0.01, 0.05, and 0.1 g, respectively, with a comparison being made between the catalytic activities for each formulation of the bifunctional catalyst.The results show that the catalyst with the highest activity to hydrocarbon transformation is the formulation with 20% of zeolite USY/Al2O3 with a percentage of 0.01% Pt (Figure 5). Since at higher percentages, the metallic phase does not allow the transition towards the acid phase, which results in a rapid saturation of the free fatty acids not allowing molecular cracking reactions [26]. The total triglyceride conversion is proportionality to temperature. At 310°C, conversion levels reach 20% with 0.01% Pt loaded; at 350°C, conversion levels increase until 40%; and finally at 390°C, conversion levels increase to 75% at WHSV 35.3 h−1.Figure 5
Comparative catalytic activity in samples hydrotreated by FTIR at different temperatures and WHSV with platinum-loaded 20% USY/Al2O3 catalyst. (black square) 0.01% Pt WHSV = 176.4 h−1; (light gray square) 0.01% Pt WHSV = 35.28 h−1; and (dark gray square) 0.05% Pt WHSV = 35.28 h−1.


## 3.2. CG/MSD

A comparative study of the degree of reaction progression by FTIR and CG/MSD was carried out, where it was observed (Figure6) that there is a higher degree of advancement by FTIR compared to CG/MSD for the same samples; with increasing temperature at 390°C, there is a significant difference between the yields for the same catalyst formulation.Figure 6
Comparative maximum conversion and hydrotreated samples by FTIR and CG/MSD at different temperatures with catalyst 0.01% Pt and 20% USY/Al2O3 at WHSV = 35.28 h−1.Despite this, both analytical techniques coincide in the formulation of the catalyst with 20% of zeolite USY/Al2O3 with a percentage of 0.01% Pt as the formulation of greater activity in the hydrotreatment process. The discrepancies in absorbance values obtained by FTIR are overestimated by the presence of compounds with similar C = O binding. This is attributed to the formation of light fatty acids of lower molecular weight compared to the initials present in the triglyceride. It is known that in the process, hydrotreating occurs first before hydrocracking [27]. Whereby at a temperature of 310°C, there is more hydrogenation/dehydrogenating activity than acidic activity [28].By FTIR analysis, the light fatty acids considered them as reactive for keeping the C=O bond current, while for CG/MSD, they were considered as reaction intermediates since they are not part of the initial triglyceride. This difference is observable for each operating temperature performed in this work, where there is the presence of other functional groups that makes the reaction follow-up similar by both techniques.The formation of partially deoxygenated groups increases as temperature and WHSV increase; these compounds are considered as primary intermediates of reaction of the free fatty acids to olefins and as by-products of reaction to the alkanes and aromatics as a result of processes of cyclization and hydrogenation of the olefins [29]. The hydrocarbon cuts formed have a high selectivity towards the formation of chains of the order of diesel and in less amount hydrocarbon formation of the order of jet fuel and gasolines in a proportion of 6 : 1 and 21 : 1, respectively, Figures 6, 7, and 8.Figure 7
Catalytic activity forJatropha curcas L. seed oil. Catalytic selectivity in functional groups for bifunctional catalyst 0.01% Pt and 20% USY/Al2O3 at WHSV = 35.28 h−1.Figure 8
Yield in hydrocarbon cuts as a function of temperature and WHSV with bifunctional catalyst 0.01% Pt and 20% USY/Al2O3.It is clearly observed that at a temperature of 390°C, there is a higher formation of hydrocarbons of the order of diesel with a yield of more than 35%, while for jet fuel and gasolines are maintained at yields of less than 10%; this emphasizes that the catalyst is selective to cuts of diesel. Similar results have been reported by Zheng et al. [16] and Li et al. [15] who reported similar conversions of 68.6% and 58.7% of liquid products, respectively, at higher WHSV and temperature values compared with those used in this research.


## 4. Conclusions

The bifunctional catalyst synthesized showed high activity in the hydrotreatment ofJatropha curcas seed oil with a selectivity towards linear hydrocarbon chains; the activity increases as a function of temperature and space velocity but with a decrease in the selectivity towards hydrocarbon chains of the order of the diesel.The selectivity towards the formation of saturated fatty acids was increased with platinum loading percentages of 0.01 wt% on the surface of the catalyst responsible for the hydrogenating activity, resulting in a decrease in acid activity. The formulation of the catalyst that showed the highest activity in high molecular weight hydrocarbon cuts is (0.01%) Pt and (20%) USY/Al2O3 for both process monitoring techniques.USY zeolite is very active and selective as hydrotreated catalyst, even at moderate conditions, and that can be attributed to its acidity function, which is strong enough to accelerate this reaction. Pt incorporation in the zeolite is greatly effective for enhancing the transformation ofJatropha curcas seed oil and for improving the selectivity to the linear hydrocarbons reaction.



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*Source: 5326456-2018-04-23.xml*