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Bulletin of Chemical Reaction
Bulletin
of Chemical
Reaction
Engineering
& Catalysis
Engineering & Catalysis
ISSN
ISSN1978-2993
1978-2993
Volume 5, Number 1, Year 2010, May 2010
Available
online at: http://www.undip.ac.id/bcrec
An Electronic
International
Journal. Available online at: http://bcrec.undip.ac.id/
Chemical Reaction
Engineering & Catalysis
(CREC) Group
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Department of
Chemical Engineering,
DIPONEGORO
UNIVERSITY
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Masyarakat Katalisis
Indonesia—Indonesian
Catalyst Society
(MKICS)
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ORIGINAL OFFPRINT OF BCREC ARTICLES
Sec ondar y Stor yH eadline
Bull. Chem. React.
Eng. Catal.
Vol. 5
No. 1
1 - 62
Semarang
May 2010
ISSN
1978 -2993
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I. Istadi, B. Pramudono, S. Suherman, and S. Priyanto, (2010). Potential of
LiNO3/Al2O3 Catalyst for Heterogeneous Transesterification of Palm Oil to
Biodiesel. Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1): 5156. (DOI: 10.9767/bcrec.5.1.777.51-56)
Published by:
Department of Chemical Engineering, Diponegoro University
Bull. Chem. React.
Vol. 3
No. 1-3
Masyarakat
Eng. Catal. Katalis Indonesia —
Semarang
ISSN
1— 62
Indonesian
Catalyst2008
Society (MKICS)
1978-2993
December
Available online at BCREC Website: http://bcrec.undip.ac.id
Bulletin of Chemical Reaction Engineering & Catalysis, 5(1), 2010, i
EDITORIAL BOARD
EDITOR-IN-CHIEF:
Dr. I. Istadi
Department of Chemical Engineering, Diponegoro University, Jln. Prof. Soedarto, Kampus Undip Tembalang, Semarang, Central Java,
Indonesia 50275; E-mail: [email protected] ; (SCOPUS h-index: 8)
ASSOCIATE EDITOR:
Prof. Dr. P. Purwanto, Department of Chemical Engineering, Diponegoro University, Jln. Prof. Soedarto, Kampus UndipTembalang,
Semarang, Indonesia 50275
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Dr. Didi Dwi Anggoro, Department of Chemical Engineering, Diponegoro University, Jln. Prof. Soedarto, Kampus Undip Tembalang,
Semarang, Indonesia 50275, (SCOPUS h-index: 3)
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Dr. Mohammad Djaeni , Department of Chemical Engineering, Diponegoro University, Jln. Prof. Soedarto, Kampus Undip Tembalang,
Semarang, Central Java, Indonesia 50275, (SCOPUS h-index: 3)
MANAGING EDITOR FOR ASIA-PACIFIC:
MANAGING EDITOR FOR EUROPE:
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Prof. Dr. Y. H. Taufiq-Yap , Centre of Excellence for Catalysis Science and Technology, Faculty of Science, Universiti Putra
Malaysia, 43400 UPM Serdang, Selangor, Malaysia, Malaysia ; (SCOPUS h-index: 12)
Prof. Dr. Dmitry Yu. Murzin, Laboratory of Industrial Chemistry and Reaction Engineering, Abo Akademi University; Biskopsgatan 8
20500, Turku/Åbo, Finland, ph: + 358 2 215 4985 fax:+ 358 2 215 4479, Finland ; (SCOPUS h-index: 32)
INTERNATIONAL ADVISORY EDITORIAL BOARDS
Prof. Dr. Nor Aishah Saidina Amin
Chemical Reaction Engineering Group (CREG), Faculty of Chemical
and Natural Resources Engineering, Universiti Teknologi Malaysia,
81310 UTM Skudai, Johor, Malaysia , (SCOPUS h-index: 10)
Prof. Dr. Raghunath V. Chaudhari
Center for Environmental Beneficial Catalysis, Department of
Chemical and Petroleum Engineering, The University of Kansas,
1501 Wakarusa Dr., Building B-Room 112B, Lawrence, KS 660471803, USA, (SCOPUS h-index: 25)
Prof. Dr. Hadi Nur
Ibnu Sina Institute for Fundamental Science Studies, Universiti
Teknologi Malaysia , 81310 UTM Skudai, Johor, Malaysia, (SCOPUS
h-index: 10)
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Prof. Dr. Mostafa Barigou
School of Chemical Engineering, University of Birmingham,
Edgbaston, Birmingham B15 2TT, United Kingdom, (SCOPUS hindex: 16)
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Dr. Satish Lakhapatri
Process Engineering Department, Siluria Technologies, San
Francisco, California, USA, (SCOPUS h-index: 2)
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Dr. Sibudjing Kawi
Department of Chemical and Biochemical Engineering, National
University of Singapore, Singapore, (SCOPUS h-index: 26)
Prof. Dr. Ram Prasad
Department of Chemical Engineering and Technology, Institute of
Technology, Banaras Hindu University, India (SCOPUS h-index:3)
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Dr. S. Subagjo
Department of Chemical Engineering, Institut Teknologi Bandung, Jl.
Ganesha 10, Bandung, Indonesia
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Prof. Dr. Abdullah M. Busyairi
Department of Chemical Engineering, Diponegoro , University,
Semarang, Indonesia, Jln. Prof. Soedarto, Kampus Undip
Tembalang, Semarang, Central Java, Indonesia 50275
Prof. Dr. Liu Yan
School of Chemical Engineering , Qinghai University, Xining, China
Email: [email protected]
Dr. Yang Hong
Dalian Institute of Chemical Physics, Chinese Academy of Sciences,
457 Zhongshan Road, Dalian 116023, China; E-mail:
[email protected]
Prof. Dr. Abdul Rahman Mohamed
School of Chemical Engineering, Universiti Sains Malaysia, 14300
Nibong Tebal, Pulau Penang, Malaysia, SCOPUS h-index: 26)
Dr. Hery Haerudin
Research Center for Chemistry, Indonesian Institute of Sciences (PP
Kimia – LIPI), Kawasan PUSPIPTEK, Tangerang, Banten, Indonesia
(SCOPUS h-index: 1)
Dr. Oki Muraza
CENT & Department of Chemical Engineering, King Fahd University
of Petroleum and Minerals (KFUPM), PO Box 5040 Dhahran 31261
KSA, Saudi Arabia , (SCOPUS h-index: 4)
Dr. K. Kusmiyati
Department of Chemical Engineering, Department of Chemical
Engineering, Muhammadiyah University of Surakarta,
Pabelan, Surakarta, Indonesia, Telp/Fax: +62-271-717417, Indonesia
(SCOPUS h-index: 2)
Dr. Heru Susanto
Department of Chemical Engineering, Diponegoro University,
Indonesia, SCOPUS h-index: 9)
Prof. Dr. Xian-ji Guo
Department of Chemistry, Zhengzhou University, Zhengzhou 450052,
China, (SCOPUS h-index: 4)
Dr. Yibo Zhou
Department of Chemistry, Iowa State University, Ames, IA 500113111,United States, Phone: 1-515-294-6986, United States, SCOPUS
h-index: 7)
Copyright © 2010, BCREC, ISSN 1978-2993
Available online at BCREC Website: http://bcrec.undip.ac.id
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 51 - 56
Potential of LiNO3/Al2O3 Catalyst for Heterogeneous
Transesterification of Palm Oil to Biodiesel
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I. Istadi *, B. Pramudono, S. Suherman, and S. Priyanto
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Department of Chemical Engineering, Diponegoro University, Jl. Prof. Sudharto,
Kampus UNDIP Tembalang, Semarang 50239, Indonesia
Received: 24 April 2010; Revised: 20 May 2010; Accepted: 21 May 2010
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Abstract
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Production of biodiesel through transesterification process using heterogenous catalysts in order to avoid
the saponification problem was studied. In this process, palm oil reacted with methanol to form a mixture
of glycerol and biodiese over a solid basic catalyst. One type of the catalysts used in this research is basic
catalyst of LiNO3/Al2O3. The parameters studied in this research are concentration of LiNO 3 loading on
Al2O3 and effect of different reaction time. The products was analyzed using Gas Chromatography to determine composition and yield of resulted methyl esters as well as conversion of palm oil to biodiesel. The major products in this transesterification reaction were biodiesel and glycerol. It can be concluded that the 20
wt% LiNO3/Al2O3 catalyst is potential for producing biodiesel from palm oil over transesterification reaction. Advantages of the usage of this catalyst is that the soap formation was not observed in this research.
© 2010 BCREC UNDIP. All rights reserved
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Keywords: Biodiesel; heterogenous catalyst; superbasic catalyst; transesterification; palm oil
1. Introduction
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Due to the increase in crude oil prices and
environmental concerns, a search for alternative
fuels has gained recent significant attention.
Among the different possible resources, diesel fuels
derived from triglycerides of vegetable oils and
animal fats have shown potential as substitutes for
petroleum-based diesel fuels. However, the direct
use of vegetable oils in diesel engine can lead to a
number of problems such as poor fuel atomization,
poor cold engine start-up, oil ring stickening and
the formation of gum and other deposits.
Consequently, considerable efforts have been made
to develop alternative diesel fuels that have the
same properties and performance as the
petroleum-based fuels [1]. In addition, biodiesel is
better than diesel fuel in terms of sulfur content,
flash point, aromatic content and biodegradability.
The direct usage of vegetable oils as biodiesel is
possible by blending it with conventional diesel
fuels in a suitable ratio. But direct usage of these
triglyceride esters (oils) is unsatisfactory and
impractical for long term usages in the available
diesel engines due to high viscosity, acid
contamination, free fatty acid formation resulting
in gum formation by oxidation and polymerization
and carbon deposition. Hence vegetables oils are
processed so as to acquire properties (viscosity and
* Corresponding Author.
E-mail address: [email protected] (I. Istadi),
Tel: +62-24-7460058, Fax: +62-24-76480675
bcrec_008_2010 Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 52
2. Materials and Methods
2.1. Materials of Research
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The materials used in these experiments are
methanol, cooking oil, lithium nitrate and
aluminium oxide. Cooking oil was supplied by
Swalayan Ada (Bimoli). The average molecular
weight of palm oil was taken as 820 g/mol and
density as 0.88 g/ml at 20 oC. Methanol (99%) was
purchased from Grade AR while lithium nitrate
(99.995 %) and aluminium oxide were supplied by
Merck.
2.2. Catalyst Preparation
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The LiNO3/Al2O3 catalyst was prepared by
impregnation method. A certain amount of lithium
nitrate was dissolved in distilled water to be a 1 N
solution. A certain amount of powdery alumunium
oxide was immersed into an aqueous solution of
lithium nitrate for 2 h at ambient temperature.
The mixed chemicals was dried overnight in an
oven (Memmert) at 393 K. Next, the powder was
calcined at 1123 K in a muffle furnace (Carbolite)
for 4 h and then crushed into the desired size (45–
60 mesh).
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volatility) similar to that of fossil fuels and the
processed fuel can be directly used in the diesel
engines available. Three processing techniques are
mainly used to convert vegetable oils to fuels form,
they are pyrolysis, microemulsification and
transesterification [2-5].
There are four primary ways to make biodiesel
which are direct use and blending, microemulsions,
thermal cracking (pyrolysis) and transesterification. The most common way to produce
biodiesel is by transesterification. In the
transesterification, triglycerides in vegetable oil
react with alcohol to form a mixture of glycerol and
fatty acid alkyl esters, called biodiesel. If methanol
is used, the resulting biodiesel is fatty acid methyl
ester (FAME), which has proper viscosity, boiling
point and high cetane number. Methanol is the
commonly used alcohol in this process, due to its
low cost.
Transesterification can be catalyzed by both
acidic-and basic-catalysts. Currently from the
literature review, most of the biodiesel are
synthesized using alkaline catalysts because the
transesterification reaction by an acid catalyst is
much slower than that by the alkaline catalysts.
However, in the alkaline metal hydroxidecatalyzed transesterification, even if a water-free
vegetable oil and alcohol are used, a certain
amount of water is produced from the reaction of
the hydroxide with alcohol. The presence of water
leads to the hydrolysis of the esters and formed a
lot of soap. The formation of soap reduces the
biodiesel yield and causes significant difficulty in
product separation (ester and glycerol). To avoid
the problem of products separation and reduces the
biodiesel yield, it has been proposed to replace the
homogeneous catalysts by a heterogeneous
catalysts. The second conventional way of
producing biodiesel is using an acid catalyst
instead of a base. Any mineral acid can be used to
catalyze the process; the most commonly used
acids are sulfuric acid and sulfonic acid. Although
yield is high, the acids, being corrosive, may cause
damage to the equipment and the reaction rate
was also observed to be low [3].
This research is purposed to study the
transesterification of palm oil into biodiesel using
LiNO 3 /Al 2 O 3 heterogeneous catalyst. The
production of biodiesel was investigated in this
research using basic solids catalyst as
heterogeneous catalysts.
The
usage
of
heterogeneous catalysts in the biodiesel production
may result in high content, high yield of methyl
esters and conversion of oil. The soap formation
was not observed which will increase the
production of biodiesel.
2.3. Catalyst Testing
The transesterification reaction carried out in a
500 cm3 reactor vessel. The oil, the methanol and
the catalyst were filled in the reactor. The mixed
reactants were stirred which sufficient to keep
uniform in temperature and catalyst distribution.
The reactor temperature was controlled by a
temperature controller. The system temperature
was raised to 60 oC and maintained at this
temperature for the needed reaction time. Thus,
the reactor was cooled to room temperature. After
cooling, the catalyst was separated from the
product mixture by vacuum filtration. The glycerol
phase (bottom layer) and the methyl esters
biodiesel phase (top layer) were separated and put
in a separate container.
The biodiesel products were analyzed in a gas
chromatography mass spectrometry (GC-MS),
equipped with a capillary column (Agilent 1901 S433, 30 m x 250 µm x 0.25 µm) and a mass
selective detector (MSD). This GC-MS was
controlled by a PC with a software package (MSD
Chemstation). Helium was used as a the carrier
gas with the flowrate at 2.2 ml/min. The injector
temperature is at 80 oC and the maximum oven
temperature is 300 oC. Analysis of biodiesel for
each sample was carried out by dissolving 1 ml of
biodiesel sample into 5 ml of n-hexane and
Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 53
injecting 0.2 µl of this solution in GC. The methyl
esters content, methyl esters yield and conversion
in each experiment were calculated from their
content in biodiesel as analyzed in GC.
.
3. Results and Discussion
3.1. Product of Transesterification of Palm
Oil
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Transesterification process of palm oil to
biodiesel over LiNO3/Al2O3 catalyst produced liquid
products consisted of two layers. The bottom layer
is a glycerol, while the top one is a methyl ester.
Figure 1 shows the two layer of reaction product of
transesterification process. This two phases were
separated depends on their layer.
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Figure 2. Effect of LiNO3 loading of oil conversion.
Reaction conditions : methanol/oil molar ratio 6:1,
catalyst amount = 1%, reaction time = 1 h, reaction
temperature = 60 oC.
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As shown in Figure 2, when the loading amount
of LiNO3 increased, the conversion of 38.4 % was
registered at loading of 20 wt%. However, if the
loaded LiNO3 was over 20 wt%, the conversion
decreased. The conversions of 25.5 %, 17.06 % and
5.9 % were obtained for 25 wt%, 30 wt% and 35
wt% of LiNO3 loading, respectively. Meanwhile,
the conversions of 0% were obtained at loading
LiNO3 of 10 wt% and 40 wt%. It is very likely that
dispersion of LiNO3 on Al2O3 support weakens the
combination of Li+ and NO3- ions due to the
interaction between LiNO3 and the surface of
support, which is beneficial for the decomposition
of LiNO3. At low loading of LiNO3 which is 10 wt%,
the sample did not present any catalytic activity,
due to the lack of strong basic sites on which
methanolysis reaction could occur.
When the amount of LiNO3 loadings were
increased more than 10 wt%, the active basic sites
are more dispersed on the alumina surface and
strong adsorption of reactant may occur at
unreactive surface sites [6]. However, if alumina
was loaded too much with LiNO3, the component
cannot be well dispersed. The amount of loaded
LiNO3 higher than 20 wt% resulted in
agglomeration of the active LiNO3 phase and the
cover basic sites by the exceeded LiNO 3, hence
lower the surface areas of active components. The
excess LiNO3 cause a lowered catalytic activity.
Therefore, it seemed that the catalytic activity was
proportional to the total loading amount of LiNO 3.
Among this investigation, the loading of 20 wt%
LiNO3 on alumina has shown promising results
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Figure 1. Product of transesterification process
of palm oil and methanol
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3.2. Effect of LiNO3 Loading on Oil
Conversion
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On account of the high activity of the catalysts
in the transesterification reaction of palm oil,
influence of loading amount of LiNO3 on
conversions of triglycerides were studied to find a
higher catalytic catalyst. Figure 2 shows the effect
of the loading amount of LiNO3 on the conversion
of palm oil at the loading amount range 10 to 40
wt%. Loading of LiNO3 onto the Al2O3 produced a
dramatic increment of basic strengths on the
LiNO3/Al2O3 leading to enhancing transesterification mechanism and increasing methyl
esters formation.
Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 54
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Figure 3 shows methyl esters content as
function of LiNO3 loading, while Figure 4 presents
yield of methyl esters over the variation of LiNO 3
loading on alumina. The methyl ester was not
observed when 10 wt% of LiNO 3 supported into
alumina was used in this transesterification. This
is also similar as in the case using 40 wt% of LiNO 3
loading on alumina. From the figure, 20 wt% of
LiNO3/Al2O3 provides the highest content of methyl
ester closes to 97.8 wt%. In comparison with 25
wt%, 30 wt% and 35 wt% of LiNO3 loading, the
loadings give the lower methyl ester content. The
methyl ester content of 35.89 wt% was obtained if
25 wt% of LiNO3 loading was used. Whereas
methyl ester content of 28.13 wt% was obtained
using 30 wt% and 9.2 wt% was obtained using 35
wt% of LiNO3 supported on alumina. Therefore,
the experimental run using 20 wt% of LiNO 3
loading on alumina at 1 hour of rection time and 60
oC of reaction temperature gives a promising
biodiesel product. The potential performance
occurs may be due to the good formation of strong
basic sites on the catalyst therefore soap formation
did not occur in the product of methyl ester. It can
be concluded that 1 hour of reaction time is
sufficient to purify the methyl ester product.
The results of methyl ester yield were shown in
Figure 4. Trend of the graph is similar with methyl
ester content which is the upward trend in the
methyl ester yield if the loading bigger than 10
wt% and the downward trend is observed if the
loading bigger than 20 wt% of LiNO3. The methyl
ester yield of 0 wt% was observed when the
transesterification were run using below 10 wt%
and higher than 40 wt% of LiNO3 loadings.
The highest methyl ester yield of 40.86 wt% was
obtained using 20 wt% of LiNO 3 loading on
alumina compared with another one. This is
similar with the result of methyl ester content
where 20 wt% of LiNO3 loading gives the highest
methyl ester content. The methyl ester yield for 25
wt% loading is 25.2 % whereas the yield of 18.02
wt% and 6.4 wt% is obtained for 30 wt% and 35
wt% of LiNO3 loading, respectively.
From the result, there is no catalytic activity for
LiNO3 loading of lest than 10 wt% and higher than
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3.3. Effect of LiNO3 Loading on Methyl Ester
Content and Yield
40 wt% due to lack of strong basic sites. The parent
of alumina is slight acidic and when the amount of
LiNO3 is loaded, the catalyst basicity is increased.
However, when the loaded LiNO3 is over 20 wt%,
the yield is decreased which may be due to the
LiNO3 cannot be well dispersed on alumina
support. The excess LiNO3 loading could cover the
basic sites on the surface of composite and cause a
lowered catalytis activity. Therefore, it seems that
the catalytic activity is proportional to the amount
of decomposed LiNO3 instead of the total loading
amount of LiNO3 [6].
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when used as a heterogeneous catalyst for the
transesterification of palm oil with methanol since
it gives higher methyl esters contents and yields.
Hence, the loading of 20 wt% of LiNO 3 on alumina
would be needed for further investigation
particularly for catalyst characterization.
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Figure 3. Effect of LiNO3 loading on methyl esters
contents. Reaction conditions: reaction time = 1 h,
reaction temperature = 60 oC
Figure 4. Effect of LiNO3 loading on yield of
methyl esters. Reaction conditions: reaction time =
1 h, reaction temperature = 60 oC
Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 55
Among this investigation whereby the influence
of loading amount of LiNO3 on the methyl ester
content and yield to find a higher catalytic activity,
the loading of 20 wt% LiNO3 on Al2O3 shown
promising results closely matching the effects of
LiNO3 loading on the conversion of triglycerides.
Therefore, it is interesting to further investigate
the parameters affecting the transesterification
catalyzed by 20 wt% of LiNO3/Al2O3 including all
parameters interaction.
of methanol into beef tallow but from one to five
minutes, the reaction proceeded very fast.
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Figure 5. Effect of reaction time on oil conversion
and methyl esters yield. Reaction conditions :
methanol/oil molar ratio 6:1, catalyst amount =
1%, reaction temperature = 60 oC, LiNO3 loading =
20 wt%
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As shown in Figure 5, trend of reaction time on
oil conversion is similar with that towards yield of
methyl ester. By using the 20 wt% LiNO 3/Al2O3
catalyst, the conversion reachs nearly constant
after 4 hours reaction time. Based on Xie et al. [6],
transesterification of soybean oil catalyzed by
potassium loaded on alumina as a solid-base
catalyst was studied. This paper reported that the
conversion is increased in the reaction range
between 1 and 7 hours, and thereafter remained
nearly constant. That’s mean the results is similar
with the results of Xie et al. [6].
The reaction was very fast in the first few hours
where the conversion increased rapidly and a
product of closed to 100 % of ester content was
formed within first 3 hours. After that, the reaction
slowed down and entered a slow rate stage till the
reaction equilibrium was reached eventually.
According to Ma and Hanna [7], conversion
increases with reaction time. It can be concluded
that reaction time is also a controlling factor of
product yield and extending the reaction time has
a positive effect on the product yield in term of
heterogenous catalytic transesterification.
From Figure 5, the methyl ester content closed
to 100% at a reaction time of 1 hour and then
remained relatively constant with increasing
further reaction time. The purity of biodiesel
reached equilibrium after 1 hour reaction time
using 20 wt% of LiNO3 on Al2O3. The constant
value obtained is due to the reaction will proceed to
near completion even at room temperature if given
enough time [8]. In term of methyl esters yield,
increasing yield during the first hour to 4 hours is
due to the mixing and dispersion of methanol into
oil and then the reaction proceed to near
completion. It can be concluded that the ester yield
slightly increases as the reaction time increases.
Ma [9] studied the effect of reaction time on the
transesterification of beef tallow with methanol.
He reported that the reaction is very slow during
the first minute due to the mixing and dispersion
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3.4. Effect of Reaction Time on Oil
Conversion and Methyl Esters Yield
3.5. Characterization of Biodiesel Product
Further investigations on the physical
properties of biodiesel were studied. The highest
yield of biodiesel obtained from these experiments
which are reaction time at 5 hours, reaction
temperature at 60 oC and using 20 wt%
LiNO3/Al2O3 was taken a sample for product
characterization. The properties of this sample was
compared with biodiesel standards. The
characterization result is presented in Table 1.
Viscosity value of standard is specified by
ASTM D 445 method, while density and iodine
values are specified by DIN 51606 method. From
the table, the viscosity value of the sample was
0.72 mm2/s, while the range of biodiesel standard
is around 1.9-6.0 mm2/s which means it is not
under the range of biodiesel standard. The density
value obtained was 0.79 kg/l while for biodiesel
standard is around 0.875-0.9 kg/l which is also not
within the limit of biodiesel standard. Meanwhile,
the iodine value was 3.8 mg I2/g which is within
the range of biodiesel standards.
From the value of viscosity, it can be said that
this sample is good due to the lower viscosity
because high viscosity leads to poorer atomization
of the fuel spray and less accurate operation of the
Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5 (1), 2010, 56
3
Density (kg/m )
Iodine Value
(mg I2/g)
Biodiesel
(Standard)
Biodiesel
(Sample)
D 445
1.9 - 6.0
0.72
DIN
51606
0.875 - 0.9
DIN
51606
<15
0.79
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[1] Jitputti, J., Kitiyanan, B., Rangsunvigi,. P., Bunyakiat,
K., Attanatho, L. and Jenvanitpanjakul, P. (2006).
Chem. Eng. J. 116 : 61-66.
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[2] Ma, F., Hanna, M.A. (1999), Bioresour. Technol., 70:
1–15
[3] Ranganathan, S.V., Narasimhan, S.L., Muthukumar,
K. (2008), Bioresour. Technol., 99: 3975–3981
[4] Marchetti, J.M., Miguel, V.U., Errazu, A.F. (2006),
Renew. Sustain. Energy Rev. 11:1300-1311
[5] Meher, L.C., Sagar, D.V., Naik, S.N. (2006), Renew.
Sustain. Energy Rev., 10:248–268
[6] Xie, W., Peng, H. and Chen, L. (2006). App. Catal. A
300 : 67-74
[7] Ma, F. and Hanna, M. A. (1999). Bioresour. Technol.
70 : 1-15
[8] Li, H. and Xie, W. (2005). Catal. Lett. 107 : 25-30
3.81
[9] Ma, F. (1998). Biodiesel fuel: The transesterification
of beef tallow. University of Nebraska-Lincoln : PhD
dissertation
[10] Demirbas, A. (2005). Prog. Energy Combust. Sci. 31:
466-487
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The major fatty acid methyl ester components were
detected by GC-MS which are palmitic acid, oleic
acid, stearic acid and linoleic acid.
4. Conclusion
References
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Viscocity @ 40
o
C (mm2/s)
Method
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Parameters
The authors would like to express their sincere
gratitudes to Department
of Chemical
Engineering, Faculty of Engineering, Diponegoro
University for the financial support received under
the project of HIBAH PENELITIAN JURUSAN
TEKNIK KIMIA 2010.
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Table 1: Comparison of physical properties of
sample biodiesel with standard biodiesel
Acknowledgments
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fuel injectors. The density value obtained from this
experiment was much lower than the standards.
Demirbas [10] reported that the density values of
vegetable oil methyl esters considerably decreases
via transesterification process.
In this research, the iodine value obtained was
3.81 g I2/g sample which is under the biodiesel
standard value. Since the iodine value was only
dependent on the origin of the vegetable oil, the
biodiesel esters obtained from the same oil should
have similar iodine values. The iodine value of the
conventional diesel fuel is approximately 10.
Therefore, the biodiesel has a significantly higher
degree of unsaturation than diesel fuel. From the
results obtained, we can conclude that the viscosity
and the density values of this sample were not
meet the requirement of the biodiesel standards
while the iodine value was meet the requirement.
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The results indicated that biodiesel could be
produced via transesterification of palm oil using
basic solid catalyst which based on LiNO 3/Al2O3 as
heterogenous catalyst. The soap formation was not
observed in this research, which reduces the
production of biodiesel. The 20 wt% loading of
LiNO3 on Al2O3 was sufficient for producing methyl
ester content with promising yield. The 5 hours of
reaction time gave the highest methyl ester yield
and conversion of oil to biodiesel. The major fatty
acid methyl ester components were detected by
GC-MS which are palmitic acid, oleic acid, stearic
acid and linoleic acid.
Copyright © 2010, BCREC, ISSN 1978-2993
Available online at BCREC Website: http://bcrec.undip.ac.id
Bulletin of Chemical Reaction Engineering & Catalysis, 5(1), 2010, iii
INDEXING AND ABSTRACTING
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Copyright © 2010, BCREC, ISSN 1978-2993
Bulletin of Chemical Reaction Engineering & Catalysis, 5(1), 2010, iv
TABLE OF CONTENTS
1. Aims and Scope ……………………………………………………………………………………. (i)
2. Indexing and Abstracting …………………………………………………………………………(i)
3. Editorial Board ……………………………………………………………………………………..(ii)
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4. Preface ……………………………………………………………………………………………… (iii)
5. Table of Content ………………………………………………………………………………….. (iv)
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6. Production of Biodiesel from Oleic Acid and Methanol by Reactive Distillation (Kusmiyati,
and Agung Sugiharto ) …...…………………………………………. …………………….. (1 - 6)
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7. Preparation Methods and Applications of CuO-CeO2 Catalysts: A Short Review (R. Prasad,
and Gaurav Rattan ) .................................................................................................... (7 - 30)
8. Hydrodynamic Studies on a Trickle Bed Reactor for Foaming Liquids (Renu Gupta and Ajay
Bansal ) ……………………………………………………………………………………… (31 - 37)
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9. Mixed Oxide Supported MoO3 Catalyst: Preparation, Characterization and Activities in Nitration of o-xylene (S.M. Kemdeo, V.S. Sapkal 1, G.N. Chaudhari) ...…………….... (39 - 49)
10. Potential of LiNO3/Al2O3 Catalyst for Heterogeneous Transesterification of Palm Oil to Biodiesel (I. Istadi, B. Pramudono, S. Suherman, and S. Priyanto ) ...…………………...(51 - 56)
11. Author Guidelines
…………………….……...…………………………..………….. (57 - 59)
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13. Submission Information
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12. Copyright Transfer Agreement ………………………………………………………….. (60 - 61)
Copyright © 2010, BCREC, ISSN 1978-2993