Accepted Manuscript

Title: Effect of Different Catalysts on the Cracking of JatrophaOil

Author: Shelly Biswas D.K. Sharma

PII: S0165-2370(14)00250-2DOI: http://dx.doi.org/doi:10.1016/j.jaap.2014.10.001Reference: JAAP 3304

To appear in: J. Anal. Appl. Pyrolysis

Received date: 11-2-2014Revised date: 1-10-2014Accepted date: 1-10-2014

Please cite this article as: S. Biswas, D.K. Sharma, Effect of Different Catalysts onthe Cracking of Jatropha Oil, Journal of Analytical and Applied Pyrolysis (2014),http://dx.doi.org/10.1016/j.jaap.2014.10.001

This is a PDF file of an unedited manuscript that has been accepted for publication.As a service to our customers we are providing this early version of the manuscript.The manuscript will undergo copyediting, typesetting, and review of the resulting proofbefore it is published in its final form. Please note that during the production processerrors may be discovered which could affect the content, and all legal disclaimers thatapply to the journal pertain.

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Highlights

• Catalytic cracking of Jatropha oil

• Formation of 36 % gasoline range hydrocarbons (C7 to C11) and 58 % diesel range

hydrocarbons(C12-C22) in the cracked liquid when catalyst ZSM-5+SiAl is used

• The use of catalyst had a positive effect on the pH content of liquid products

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Effect of Different Catalysts on the Cracking of Jatropha Oil

Shelly Biswasa,b1 and D. K. Sharmaa

aCentre for Energy Studies, Indian Institute of Technology Delhi, New Delhi, India-110016

bDepartment of Chemistry, Vel Tech Dr RR & Dr SR Technical University, Avadi, Chennai, India-

600062.

Abstract

Conversion of non-edible plant seed oil Jatropha oil (JO) by cracking and the utilization of

cracked liquid product obtained as a transportation fuel have gained importance. Thus, an

attempt has been made to study the catalytic cracking of JO in a batch reactor. The

experiments were carried out under nitrogen atmosphere at a temperature of 375 oC. The

catalytic cracking of JO was carried out using three catalysts ZSM-5, ZSM-5+SiAl and

NiMo/SiAl. Catalyst ZSM-5+SiAl was the best catalyst used for JO cracking as it leads to the

formation of 36 % gasoline range hydrocarbons (C7 to C11) and 58 % diesel range

hydrocarbons(C12-C22) in the cracked liquid. It was also observed that the use of catalyst had

a positive effect on the pH content of the catalytically cracked liquid products.

Keywords

Cracking, Jatropha oil, catalyst, liquid product

Introduction

Due to the growing demand of renewable fuel oil source and depleting fossil fuel reserves

pyrolysis/cracking of non-edible plant seed oils and the utilization of cracked liquid product

as a transportation fuel has gained importance[1-2]. Thus, the transportation fuels are derived

1Corresponding Author: Tel: +91-8939488314, E.mail: shelly.biswas@gmail.com.

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from renewable sources, i.e. edible plant seed oil such as palm oil, soyabean oil, sunflower oil

[4-6] and non-edible oils such as cotton seed oil, rapeseed oil, karanj, Jatropha oil (JO) and

waste oils [7-12]. Vegetable oils are triglycerides moities, which contain fatty acid chains

connected to a glycerol backbone via the carboxylic group. These vegetable oils are instable,

have high viscosity and forms carbon deposits in parts of automobile engines (i.e. in diesel

engines) thus, these oils cannot be used as liquid fuels directly [9]. The drawback of

transesterification of these vegetable oils to biodiesel is use of large amounts of methanol

during transesterification and production of glycerol as a by-product [9, 13]. Thus, cracking,

catalytic cracking, hydrotreating and hydrocracking are the better means of conversion of

these vegetable oils to transportation fuels. Research work on vegetable oil cracking has been

concentrated on the edible oils such as palm oil [3], sunflower oil [5] etc. As these edible oils

are used as a food product thus it is required to carry out cracking of non-edible vegetable

oils to generate transportation fuels. Jatropha oil which is a non-edible oil can be used as a

cracking feed to generate these transportation fuel oils. Hydroprocessing, hydrotreating and

thermal cracking of Jatropha oil (JO) has been studied by researchers [8-9, 14]. The present

authors have studied the mechanism of JO under thermal cracking reactions, non-isothermal

and isothermal kinetics in TGA instrument and in a batch reactor respectively and analysed

the products obtained from thermal cracking reactions. It would be interesting to analyse the

effect of different catalyst under reactor conditions and characterize the liquid product

obtained for better understanding of catalytic cracking process. Thus, in the present work the

cracking of JO under reactor conditions in the presence of catalyst was investigated and the

liquid product obtained was analysed to study the effect of catalyst.

Experimental

Materials

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Jatropha oil (JO) was procured from Jatropha Vikas Sansthan, New Delhi. The ultimate

analysis was presented in Table 1.

Experimental preparation of the catalysts

Three catalysts were used for the catalytic cracking studies. The first catalyst, ZSM-5 with

Si/Al ratio 35 was procured from Sud Chemie India (P) Ltd. The ZSM-5 was calcined at 500

oC for 4 h to get the required catalyst. The second catalyst ZSM-5+SiAl was prepared by

physical mixing of ZSM-5 and silica alumina support (1:1 w/w). The silica alumina support

(for Si/Al ratio 45) was prepared from Aluminium secondary butoxide (Fluka analytical) and

tetraethyl ortho silicate (Acros organics) by co-precipitation method [15-16]. The required

amount of aluminium secondary butoxide was dissolved in ethanol and thoroughly mixed

with tetraethyl ortho silicate and then the mixture was stirred for 1 h, NH4OH was added drop

wise to precipitate out the mixture. The precipitated mixture was dried at room temperature

and then at 60 oC for 2 h. The dried support was then calcined at 700 oC for 3 h and then

crushed to get the prepared support. Catalyst ZSM-5+SiAl was prepared by physical mixing

of the prepared support with ZSM-5 in deionised water solution under overnight stirring

conditions. The obtained mixture was filtered, dried overnight at room temperature and then

at 60 oC for 2h. The dried catalyst was then calcined at 500 oC for 4 h to get the catalyst

ZSM-5+SiAl.

The third catalyst Ni-Mo/SiAl was prepared by impregnating silica alumina support with 4 %

Ni and 15 % Mo loading [17]. The required weight of nickel nitrate was dissolved in

deionised water and then under stirring condition required amount of ammonium molybdate

solution was added and thoroughly mixed. To this solution the silica alumina support is

added under stirring condition and the stirring continued for 1h. The resultant mixture is then

dried in a rotatory evaporator and then dried overnight at 60 oC. Then the prepared catalyst

was calcined at 500 oC for 4h. The prepared catalyst was reduced by chemical method. 4gm

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of the calcined catalyst was dissolved in 120ml of deionised water and 0.4gm of NaBH4 in

aqueous solution was added to it. The mixture was then stirred overnight and then filtered

washed copiously with deionised water and then dried under vacuum conditions to get the

reduced catalyst Ni-Mo/SiAl.

Characterization of the catalysts

The surface areas and pore volumes of the catalysts were analyzed using N2 adsorption. The

BET surface area, total pore volume and pore size distribution were determined from nitrogen

adsorption/desorption isotherms measured at −196 °C using Micromeritics ASAP 2010

apparatus [17-18]. Prior to gas adsorption measurements the catalyst was degassed at 180 °C

under high vacuum for a period of 6 h. The total pore volume was calculated at a relative

pressure of approximately 0.99. XRD pattern was obtained using a Bruker-model operated at

40 kV and 20 mA using Cu Kα radiation with a wavelength of 1.54 A°. The diffraction angle

was varied from 4° to 60° at a scan rate of 0.02°/s.

Experimental set up for the catalytic cracking reactions

Catalytic cracking of JO was carried out under nitrogen atmosphere and atmospheric pressure

using a fixed bed tubular semi-batch reactor [19]. The tubular batch reactor was fabricated in

SS304. The flow of nitrogen for the course of the reaction was maintained at 120mL/h. About

5-7g of the sample was used for the cracking reactions and shock heating conditions were

utilized to maximize the liquid yield. The temperature at which the effect of catalyst was

studied was 375 oC for duration of 10 min. The image of the reactor assembly is shown in

Fig. 1. The reactor assembly mainly consisted of the tubular batch reactor with a nitrogen

inlet as shown in Fig. 1. The outlet of the reactor was attached to a glass condenser which

was then connected to a liquid collection vessel. The feedstock material was introduced into

the reactor as soon as the reactor reached the desired temperature and kept at this temperature

for the required time intervals. The products formed during cracking are swept out of the

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reactor and the condensable liquids are condensed using a condenser and then collected in the

liquid sample vial as shown in Fig. 1. The residue left (char and catalyst) in the reactor vessel

is scraped out from the reactor. All the reactions were studied in triplicates. The reactions

were followed by the quantitative measurement of the products formed i.e. liquid product and

char. The amount of gaseous product formed was calculated by difference i.e. by material

balance.

The liquid products obtained from the catalytic cracking reaction were characterized

using 1H NMR spectral studies using the instrument Bruker Spectrospin 300 NMR

spectrometer. The solvent used for carrying out the NMR studies was CDCl3 containing TMS

as internal reference. The spectrum was recorded between 0-10ppm for the 1H NMR studies.

The cracked liquid was separated into different fractions by liquid column chromatographic

technique [8, 19-20]. The hexane fraction of the liquid products obtained from the cracking

reactions were characterized using GC-MS. The GC-MS was performed on the apparatus

Thermo Trace GC ultra GC-MS. The separation was conducted on a column of 25 m X 0.25

mm (ID) fused silica capillary coated with DB-5 [8, 19-20].

Results and Discussion

Catalyst characterization

The surface area, pore volume, and average pore diameter of the three catalyst used in the

study are reported in Table 2. The BET surface areas of the calcined catalysts Ni-Mo/SiAl,

ZSM-5 and ZSM-5+SiAl are 66.5, 251.7 and 113.2 m2/g respectively. Fig. 2 shows the XRD

pattern of fresh and used catalyst samples. The different peaks obtained from the XRD

pattern clearly indicate the crystalline nature of the catalyst used. The ZSM-5 and

ZSM-5+SiAl showed the typical ZSM-5 peaks in the XRD analysis (Peaks have been marked

in figure 2) [4]. From the peaks obtained in XRD analysis it was observed that there is change

in the phase of the spent catalyst after cracking reaction. Differences obtained in the peak

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intensities are related to variations in the scattering intensity of crystal components or their

arrangement in the lattice. The increased peak at ~27 for spent ZSM-5 could be due to higher

scattering of the crystal component (MFI structure) in the spent catalyst. The peaks at 8-9

correspond to the MFI structure of ZSM-5, and thus disappearance of the peaks at 8-9

indicate that cracking leads to some change in this structure. The presence of MFI structure,

Al2O3 and SiO2 corresponds to the peaks from 20-30 and the hump in 14-30 and decrease in

intensity for spent ZSM-5+SiAl might be due to X-ray shielding caused by absorption of

carbonaceous material during cracking reaction by the zeolite sample [21]. The disappearance

of peaks at 13, 23.5, 27.5, 39, 49.5 in spent Ni-Mo/SiAl may be due to X-ray shielding

caused by absorption of carbonaceous material during cracking reaction and also change in

the phase of the MoO, NiO, Al2O3 components of spent Ni-Mo/SiAl.

Reactivity of catalyst on JO cracking

The effect of different catalysts on the liquid, gaseous product and char yield for JO cracking

has been presented in Table 3. It was observed that for JO cracking NiMo/SiAl (10% catalyst

loading) was found to show about 10 % increase in the liquid yield and decrease in the

gaseous and char yield. The increase in the liquid yield indicates that 10 % catalyst loading

would be the optimum amount of the catalyst required for the maximum liquid yield. The

increase in the gaseous yield on further increasing the catalyst loading indicates that the

catalyst further increases the secondary cracking reactions leading to formation of smaller

hydrocarbons in gaseous range. Catalyst ZSM-5 catalyst had little effect on the liquid and the

gaseous yield. Catalyst ZSM-5+SiAl increased the gaseous yield and had little effect on the

liquid yield. Though the char yield increased considerably at 10 % catalyst loading, this

indicates that the presence of catalyst enhances the polycondensation and aromatization

reactions which lead to increased char formation (at lower catalyst loading this reaction is not

predominant).

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Characterization of the liquid product obtained from the catalytic cracking of JO

Definition of the 1H and 13C NMR chemical shifts for hydrocarbons and their structural

indications are given in literature [8, 22-23]. The structural parameters derived for liquid

product from the catalytic cracking of JO cracking is shown in Table 4. The liquid product

obtained from the cracking of JO at 375oC indicates the presence of 88% aliphatic hydrogen

[8], whereas it was more than 93 % for the catalytically cracked liquid product. The number

of rings (RA) in the liquid products increased in the presence of catalysts ZSM-5 and ZSM -

5+SiAl, whereas it decreased in the presence NiMo/SiAl catalyst as compared to the

thermally cracked liquid. The increase in the number of rings indicate that ZSM-5 facilitates

the aromatization reactions which increases the aromatic carbons present and decreases the

aliphatic carbons present. Increase in the aliphatic hydrogen indicates that benzene

substituted with long chain compounds are being formed in the liquid product. Even the

average chain length (ACL) decreased in presence of ZSM-5+SiAl catalyst whereas it

increased in the liquid product when cracked under the presence of ZSM-5 and NiMo/SiAl

catalysts.

Distinct absorption bands from FTIR of catalytically cracked liquid from JO cracking (Table

5 and Fig. 3) show the presence of CH3 and CH2 (2,925 cm−1), the C=O ester (1,710

cm−1),groups and whereas C-O stretch (1170 cm-1) of ester groups was absent in the liquid

product when catalyst was used for cracking.

Liquid column chromatographic technique for separation of the cracked liquid into aliphatic,

aromatics, oxygenated compounds and polar compounds were carried out. The sequence and

amount of solvents used for fractionating the different classes of compounds, and the amount

of compounds fractionated in liquid product from thermally cracked JO indicates the

presence of 86% aliphatic, 3% aromatics and oxygenated aromatics and 10% polar

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components [8]. It was observed that the toluene soluble fraction increased in the liquid

product obtained from the catalytic cracked liquid product obtained in the presence of ZSM-5

and ZSM-5+SiAl catalyst (Table 6). The increase in the toluene soluble fraction is due the

rearrangement and aromatisation reactions taking place in the presence of ZSM-5 and ZSM-

5+SiAl catalyst, which facilitate this type of reaction. But in case of Ni-Mo/SiAl, the

triglyceride molecule undergoes dehydration, decarboxylation, decarbonylation reactions.

The carbon number distribution of the liquid products obtained from the catalytic cracking

was characterized by using GC-MS studies and the results have been shown in the Table 7

and Fig. 4. Carbon number signifies the number of carbon atoms in the formula of the

compounds obtained (which relates to the diesel or gasoline fractions present) in the liquid

product. It was observed that the liquid product consisted of the different classes of organic

compounds such as alkanes, alkenes, aromatics, cycloalkanes and carboxylic acids etc. The

liquid product obtained from the catalytically cracked liquids contains both bio-gasoline and

bio-diesel range hydrocarbon when all the three catalyst are used. The liquid product obtained

from the catalytically cracked liquid of JO in the presence of ZSM-5+SiAl consisted of

gasoline range hydrocarbons (C7 to C11) of 36%, whereas the diesel range hydrocarbons (C12-

C22) formed was 58 %. Thus there is an increase in the bio-gasoline range component in the

catalytically cracked liquid product as compared to the thermally cracked liquid product

(3%). <C7 range hydrocarbons are totally absent in all the catalytically cracked liquids. The

disappearance of <C7 range hydrocarbon for all catalytic tests indicates that the secondary

cracking reactions dominant in the thermal cracking reactions have been restrained by the

primary cracking reactions in the presence of catalyst. It was observed that catalyst Ni-

Mo/SiAl led to the formation of about 20% >C22 range hydrocarbon, this could be due to

polycondensation reactions taking place during the cracking process in the presence of the

catalyst Ni-Mo/SiAl [24]. The biggest advantage of utilizing catalyst ZSM-5+SiAl as it, gives

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not only bio-diesel but also bio-gasoline range hydrocarbons in the liquid product as

compared to the thermally cracked JO. From the GC-MS analysis of the hexane fraction of

the liquid product, it was concluded that the triglyceride molecule undergoes dehydration (-

H2O), decarboxylation (-CO2), decarbonylation (-CO), recombination and rearrangement

reactions [25], to generate different hydrocarbons. The pH of the liquid products obtained

from catalytic cracking was also obtained as follows pH of liquid product obtained from JO

was 3.26 and in the presence of catalyst ZSM-5, ZSM-5+SiAl and NiMo/SiAl were 3.5, 4.1

and 3.9 respectively. It was observed that the liquid product obtained in the presence of

catalyst had a higher pH as compared to the thermally cracked liquid.

Conclusions

The effect of different catalysts on the cracking reactions of JO was studied under

atmospheric pressure and nitrogen flow. The use of 10 % NiMo/SiAl catalyst was found to

increase the liquid yield by 10% for the cracking of JO whereas ZSM-5+SiAl lead to the

formation of increased gaseous product though the liquid yield was decreased. Catalyst ZSM-

5+SiAl is the best catalyst used for JO cracking as it leads to the formation of 36 %, gasoline

range hydrocarbons (C7 to C11) and 58 % diesel range hydrocarbons(C12-C22) in the cracked

liquid. It was also observed that the use of catalyst had a positive effect on the pH content of

the catalytically cracked liquid products.

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Figure captions:

Fig. 1. Image of the cracking reactor

Fig. 2. XRD peaks for the fresh and spent catalysts

Fig. 3. FTIR absorption peaks for the liquid products obtained from cracking of JO in presence of different catalysts

Fig. 4. GC-MS chromatograms for the liquid products obtained from cracking of JO in presence of different catalysts

Table captions:

Table 1 Ultimate analysis of Jatropha oil

Table 2 Physical properties of the catalysts

Table 3 Effect of catalyst on the product distribution for JO cracking

Table 4 Average structural parameters (derived from 1H and 13C NMR data) of the liquid products obtained from cracking of JO in the presence of different catalyst (10% catalyst loading)

Table 5 FTIR absorption peaks for the samples of the liquid products obtained from cracking of JO in the presence of different catalysts (10% catalyst loading)

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Table 6 Chemical class fractionation of the cracked oil from JO cracking (in the presence of catalyst) using liquid column chromatography

Table 7 Carbon number distribution from GC-MS data observed in the liquid products obtained from catalytic cracking of JO

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Table 1 Ultimate analysis of Jatropha oil

Sample C H N S Oa Atomic

H/C

Atomic

O/C

CV

(MJ/Kg)

JO 82 13.6 0 0 4.4 1.99 0.04 46.91

aBy difference

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Table 2 Physical properties of the catalysts

Catalyst BET surface area

(m2/g)

Pore volume (cm3/g) Avg. pore diameter (Ao)

Ni-Mo/SiAl 66.5 .8± 0.04 0.002± 289.8

ZSM-5 251.7 2± 0.29 0.05± 6.5

ZSM-5+SiAl 113.2 1± 0.17 0.03± 60.7

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Table 3 Effect of catalyst on the product distribution for JO cracking

Catalyst (%) Liquid product (%) Char (%) Gaseous products (%)

0 0 73.92 1.46 24.61

ZSM-5 5 69.12 5.57 25.31

10 67.95 3.14 28.9

15 62.26 4.05 33.69

ZSM-5+SiAl 5 69.45 0.97 29.58

10 68.32 7.50 24.18

15 57.1 6.60 36.29

Ni-Mo/SiAl 5 63.27 1.21 35.52

10 82.88 0.61 16.51

15 71.75 0.27 27.97

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Table 4 Average structural parameters (derived from 1H and 13C NMR data) of the liquid

products obtained from cracking of JO in the presence of different catalyst (10% catalyst

loading)

JO Parameter

Without catalyst ZSM-5 Ni-Mo/SiAl ZSM-5+SiAl

HA 4.95 0.68 0.89 0.96

Hα 8.37 16.62 23.02 13.75

Hβ+γ 68.71 65.22 69.74 67.66

HCH3 11.46 11.31 11.95 13.03

HS 88.54 93.15 93.58 94.43

CA 6.9 9.9 10.12 9.03

CS 91.2 89.37 88.07 89.35

CPα 8.42 8.38 8.31 8.39

CPβ 8.28 9.07 8.16 8.42

CPn 23.39 42.2 32.4 6.21

CPγ 7.11 8.2 6.86 19.1

H/C 1.93 1.9 1.89 1.91

CAI 6.29 6.82 0.23 6.17

CAH 5.19 6.98 4.94 6.12

RA 2.15 4.41 1.11 4.08

ACL 11.21 16.43 13.41 10.04

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Table 5 FTIR absorption peaks for the samples of the liquid products obtained from cracking

of JO in the presence of different catalysts (10% catalyst loading)

JO Assignment Without catalyst ZSM-5 Ni-Mo/SiAl ZSM-5+SiAl

- 3851(w) - -

- 3807(w) - -

- 3727(m) 3727(m) 3727(m)

- 3699(w) 3701(m) 3701(w)

OH stretching - 3626(m) 3627(m) 3627(m)

- 3596(m) 3598(m) 3598(w)

C-H stretch alkanes 2925(s) 2925(s) 2926(s) 2925(s)

C-H stretch alkanes 2855(s) 2855(s) 2855(s) 2854(s)

C=O stretch, esters 1710(s) 1710(s) 1710(s) 1710(s)

acyclic C─C (mono-substituted alkenes)

- 1656(w) - -

C-H bend alkanes 1459(m) 1460(s) 1460(s) 1461(s)

C–H rock alkanes 1374(w) 1381(m) - 1377(m)

Wagging mode of the CH2 group

1285(m) - - 1285(m)

C–O stretch alcohols, carboxylic acids, esters, ethers

1170(w) - - -

C-C skeletal stretching modes 1114(w) 1098(m) 1099(s) 1115(w)

Vinyl group vibration - - 985(w) -

C-C skeletal stretching modes 963(m) 966(w) - 965(w)

C-H rock alkanes 723(m) 723(m) 723(m) 723(m)

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Table 6 Chemical class fractionation of the cracked oil from JO cracking (in the presence of

catalyst) using liquid column chromatography

Solvent Hexane Toluene Ethyl acetate Methanol

Volume of solvent 50ml 50ml 50ml 50ml

Fraction Aliphatics Aromatics Oxygenated

aromatics

Polar

compounds

Without catalyst 86.2 1.02 2.1 10.6

ZSM-5 21.6 45.9 22.4 10.0

Ni-Mo/SiAl 83.1 6.0 3.7 7.1

ZSM-5+SiAl 21.1 41.1 28.2 7.0

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Table 7 Carbon number distribution from GC-MS data observed in the liquid products

obtained from catalytic cracking of JO

Carbon number % distribution

JO JO (ZSM-5) JO (ZSM+SiAl) JO (Ni-Mo/SiAl)

Paraffins 23.2 - - -

Olefins 1.5 - - -

Cyclic compounds 4.8 - - - <C7

Total 29.5 - - -

Paraffins 1.3 3.05 7.31 4.79

Cyclic compounds - 4.27 5.22 4.26

Olefins 1.2 2.25 2.36 3.25

Mono-aromatics - 1.7 2.84 1.4

Acids 0.4 3.89 17.38 2.81

Alcohols - 1.81 1.07 -

C7-

C11

Total 2.9 16.97 36.18 16.51

Paraffins 8.7 7.97 8.57 12.9

Olefins - 14.4 15.9 19.6

Cyclic compounds 7.6 1.79 0.66 0.79

Acids 40.2 20.27 23.49 25.17

Alcohols 10.9 15.8 7.28 1.41

ketones - 1.31 0.89 -

Esters - 13.76 0.73 1.75

Aromatics - 0.93 - -

Di-aromatics - - - -

C12-

C22

Total 67.4 76.23 57.52 61.62

>C22 - 4.14 6.26 20.69

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Fig. 1. Image of the cracking reactor

Condenser

Reactor Assembly

Temperature Controller

Nitrogen Inlet

Thermocouple

SS Reactors

Heating Coils

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Fig. 2. XRD peaks for the fresh and spent catalysts

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722.79

1163.59

1375.08

1461.04

1744.77

2854.28

2924.53

3007.71

91

92

93

94

95

96

97

98

99

100

%T

1000 2000 3000 4000 cm-1

(a) JO cracked liquid

402.76

409.69

474.87

553.41

672.32

725.18

1093.21

1382.52

1460.31

1620.18

1655.82

1717.48

1853.21

2854.19

2923.65

3598.43

3626.87

3701.49

3727.86

3807.75

3850.26

3911.65

68

70

72

74

76

78

80

82

84

86

88

90

92

94

96

%T

1000 2000 3000 4000 cm-1

(b) JO cracked liquid (ZSM-5)

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417.44

474.83

557.43

723.51

965.68

1098.66

1380.79

1460.77

1656.39

1709.78

2854.63

2924.89

3596.95

3626.14

3699.84

3727.33

3807.22

3851.52

50

55

60

65

70

75

80

85

90

95

100

%T

1000 2000 3000 4000 cm-1

(c) JO cracked liquid ( Ni-Mo/SiAl)

472.72

723.31

964.96

1114.74

1284.87

1376.76

1461.35

1710.54

2854.90

2925.58

3598.24

3626.6537

00.93

3727.53

-0

10

20

30

40

50

60

70

80

90

%T

1000 2000 3000 4000 cm-1

(d) JO cracked liquid (ZSM-5+SiAl) Fig. 3. FTIR absorption peaks for the liquid products obtained from cracking of JO in

presence of different catalysts

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(a) JO without catalyst (b) JO (SiAl + ZSM-5)

(c) JO (ZSM-5) (d) JO (Ni-Mo/ SiAl) Fig. 4. GC-MS chromatograms for the liquid products obtained from cracking of JO in

presence of different catalysts