INTRODUCTION
Glycerol (C3H8O3) is an alcohol with three
hydroxyl groups (-OH), which can be produced as a by-product of biodiesel production
through transesterification of palm oil with alcohol (such as methanol). Methanol
is an alcohol that is familiar to use in this process because it may provide
a proper viscosity, boiling point and high cetane number of biodiesel (Fangrui
and Milford, 1999). In addition, it is more economic because of the lower
market price.
From transesterification reaction, the glycerol obtained was in crude form,
which posed a disposal problem without further purification (Yong
et al., 2001). The crude glycerol that was obtained as a by-product
from transesterification contained only about 50% glycerol in a mixture of unreacted
methanol, most of the homogeneous catalyst (NaOH) and soap. Therefore, a certain
purification steps were necessary for the crude glycerol recovery prior to be
used as a raw material in many industries and as a potential feedstock for the
production of biolubricants. Presently the conventional refinement of crude
glycerol is very expensive and complex causing it to be disqualified for high
quality uses.
For the purification techniques of crude glycerol, it may comprise steps such
as chemical treatments, crystallization, conventional filtration, microfiltration,
ultrafiltration using organic polymer membranes, treatment with ion exchange
resins, electrodialysis and vacuum distillation. Combination of two or more
of these techniques would lead to producing high purity glycerol (Buenemann
et al., 1991). Such treatments required a good understanding of the
physical as well as the chemical properties of each of the materials involved,
for example, methanol could be separated and recovered by means of vacuum distillation
(Richard and Patricia, 2004).
In this research, purification of crude glycerol deemed integral in order to
prepare the glycerol as the raw material at a biolubricant technical grade.
Any excess catalyst, salts and water could be removed by microfiltration followed
by removal of water by evaporation (Buenemann et al.,
1991). To further purifying it, gel type acidic ion exchange resin beads
would be used to eliminate fatty acid salts, inorganic salts and free ions impurities
(Rezkallah, 2008).
MATERIALS AND METHODS
Glycerol: Crude glycerol based on homogeneous catalysts, CG1 was a product of Golden Hope biodiesel plant. Crude glycerol CG2 was produced from transesterification reaction over heterogeneous catalyst. Pure glycerol reference material (PG) was purchased from Merck, Germany, with a purity content of 99.2%, as determined by HPLC.
Transesterification: Methanol and RBD palm olein (Seri Murni Brand)
were purchased from Sigma Aldrich and a local grocery shop, respectively. Characterization
of palm oil properties was shown in Table 1. These two reactants
were mixed at a molar ratio of 15:1 over a heterogeneous catalyst, 15% KOH/Al2O3
that was prepared using wet impregnation method (Noiroj
et al., 2009). The catalyst was characterized by using BET, XRD and
SEM-EDX methods. Potassium hydroxide (KOH) and γ-alumina (99.99%) were
purchase from SYSTERM and Johnson Matthey Catalog Company, respectively. The
15% KOH/Al2O3 catalyst was chosen as the transesterification
catalyst due to the high conversion and yield of biodiesel as compared to other
percent (%) loading of KOH (Baabad and Ismail, 2008).
Transesterification process was conducted in a batch reactor that consisted
of a 3-neck flask, condenser and thermometer for 2 h reaction at a reaction
temperature of 65°C with 1 wt. % of catalyst. Glycerol yielded from the
transesterification was separated from biodiesel and filtered. Unreacted methanol
was removed from crude glycerol using evaporation method. Biodiesel produced
from this reaction was at an optimum conversion of 90.54%, while glycerol was
9.46%. The heterogeneous catalysts was regenerated by immersion in hexane solvent
to remove any attached transesterification product before drying it over at
110°C for 3 h.
Crude glycerol purification
Methanol removal: For CG1 sample, excess methanol was already removed in
the Golden Hope biodiesel plant. However, for CG2 sample, excess methanol from
transesterification reaction was removed by evaporation method using rotary
evaporation at 65°C for 30 min.
| Table 1: |
Properties of the RBD palm oil |
 |
Neutralization: Five milliliter of crude glycerol samples as a product
of each of homogeneous catalyst and heterogeneous catalyst transesterification
were prepared in test tubes. Each of the sample was titrated with phosphoric
acid 85% (v/v) monitored by pH meter until it reached pH 7 using Addison method
(Addison, 2006). The amount of phosphoric acids necessary
for crude glycerol neutralization was recorded. Inorganic salts (sodium phosphate
from homogeneous reaction and other fatty acids salts) formed in the neutralization
stage were then filtered using syringe 0.45 μm filter.
Ion exchange resins method: Ion exchange resins type Amberlite IRN-78 from SUPELCO and Amberlite 200°C from Sigma Aldrich were selected to be added into the neutralized crude glycerol samples for free ions removal. Ion exchange application was performed by column technique, where the resins were placed in a vertical column chromatography to form a bed. Silica beads were also packed inside the column to remove any excess moisture content in the sample. These two types of ion exchange resins would adsorb the free anions and cations in glycerol. The used ion exchange resins were then regenerated by washing them under a flow of diluted sodium hydroxide (NaOH) for Amberlite IRN-78 and diluted sodium chloride (NaCl) for Amberlite 200°C and filtered. All the purification steps of crude glycerol for homogeneous (CG1) and heterogeneous catalyst (CG2) were summarized in Fig. 1 and 2.
|
| Fig. 1: |
Summary of purification method for crude glycerol sample based
on homogeneous catalyst (CG1) |
|
| Fig. 2: |
Summary of purification method for crude glycerol sample based
on heterogeneous catalyst (CG2) |
RESULTS AND DISCUSSION
Morphology of the fresh Al2O3 and the 15% KOH/Al2O3 catalyst were characterized by using Scanning Electron Microscope (SEM) as shown in Fig. 4a and b. K2O was found to be uniformly distributed in the 15% KOH/ Al2O3 catalyst and this was also another indication that such catalyst would promote a strong reaction towards high transesterification conversion and yield.
From BET analysis, fresh Al2O3 has a surface area of 100.4 m2 g-1. The addition of 15% KOH on the activated Al2O3 has reduced its surface area to 26.1 m2 g-1. It was shown that the active K2O components have extensively taken up nearly 75% of the Al2O3 pores hence the smaller BET surface area. This could be a good indication of the catalyst activity.
From XRD patterns shown in Fig. 3, the fresh Al2O3
showed typical diffraction peaks at 2θ = 20°, 32°, 37°,
46° and 67°. When the loading amount of KOH was increased to 15 wt.
%, the new phase of K2O can be observed at 2θ = 31°, 39°,
51°, 55° and 62°.
|
| Fig. 3: |
XRD diffractogram for fresh Al2O3 and
15% KOH/Al2O3 |
|
| Fig. 4: |
SEM micrograph for (a) fresh Al2O3 and
(b) 15% KOH/Al2O3 at 5000X magnification |
Such findings concurred with what has been reported by Xie
et al. (2006).
HPLC analysis: Samples of CG1, CG2 after purification and commercial
Pure Glycerol (PG) were analyzed using High Performance Liquid Chromatography
(HPLC) as shown in Fig. 5a-c. The HPLC conditions
were as follows: Column Dionex C18, mobile phase (acetone and acetonitrile),
flow rate (1 mL min-1), detector (ELSD) and run time (30 min).
Analysis using HPLC technique showed only one peak has been detected indicating that CG1 and CG2 samples were free from impurities such as excess catalyst, free fatty acids, methyl esters, triglyceride, diglyceride and monoglyceride after neutralization stage. Excess methanol in crude glycerol (CG2) sample was removed by evaporation method. Impurities in the neutralized glycerol samples only contained inorganic salts and free ions from salts and catalyst. These impurities have been removed once microfiltration and ion exchange resins methods were employed. As such, the chromatograms for the purified CG1 and CG2 showed a single glycerol peak each with very smooth base line that matched with the PG profile in Fig. 5.
|
| Fig. 5: |
Analysis of HPLC for (a) CG1 after purification, (b) CG2
after purification and © PG. RT = Retention time |
|
| Fig. 6: |
Analysis of FTIR for CG1 sample (1) Crude Sample before purification,
(2) after neutralization and filtration, (3) after ion exchange resins method.
PG sample labeled number 4 used as control sample |
FTIR analysis: The crude glycerols (CG1 and CG2) before and after purification were analyzed using FTIR to determine the functional groups and classes of glycerol compounds with their absorption frequencies in the infrared. There were five strecthes and bands detected in glycerol that included -OH stretch, -C-C-H bend, -C-H stretch, -C-O stretch and -CH2-OH band.
FTIR analyses of PG and CG1 before and after neutralization and filtration as well as after Step 3 were carried out and the results were depicted in Fig. 6. In CG1 sample, -COO¯ functional group was detected at frequency 1556.6 cm-1. This impurity was identified as fatty acids salt traces as a result of the reaction of the catalyst with free fatty acid. As the sample underwent step 1 and 2, such impurity could be minimized and subsequently fully removed once ion exchange resins method (i.e., Step 3) was employed.
FTIR analyses were also conducted for CG2 sample in the similar sequence as
that of CG1 and the results were shown in Fig. 7. The fatty
acids salt, which has been detected in CG2 sample in Step 1 and 2 at frequency
1557.2 cm-1 and at a very low absorbance percentage of 2%, was totally
eliminated after Step 3. This was owing to the fact that the fatty acids salt
traces from glycerol were adsorbed by the anion exchange resins.
| Table 2: |
Volume and weight amount of phosphoric acid and ion exchange
resins required in crude glycerol CG1 and CG2 purification process |
 |
In addition, the free ions from the inorganic salts have also been removed
and adsorbed by using the cation exchange resins.
The volume and weight of phosphoric acid and ion exchange resins needed in purification of CG1 and CG2 were shown in Table 2. CG2 only required 50% less amount of phosphoric acid and 60% less weight amount of ion exchange resins than CG1 to achieve the similar effect. This was another advantage of using 15% KOH/Al2O3 heterogeneous catalyst that resulted in no physical catalyst traces saved for free ions.
Once all the purification steps using neutralization, filtration and ion exchange
chromatography methods have been conducted, a few characterization tests were
carried out to determine the viscosity, pH value, free fatty acid value (Lubrizol
Standard Test Procedure, 2006) and moisture content of CG1 and CG2 before
and after purification to be compared with the commercial pure glycerol PG.
| Table 3: |
Characterization of crude glycerol based on homogeneous catalyst
(CG1) and heterogeneous catalyst (CG2) before and after purification and
pure glycerol (PG) |
 |
|
| Fig. 7: |
Analysis of FTIR for CG2 sample (1) Crude Sample before purification,
(2) after neutralization and filtration, (3) after ion exchange resins method.
PG sample labeled number 4 used as control sample |
By referring to Table 3, it was found that CG1 has a relatively
higher pH than CG2 but was comparable to that of PG. On the other hand, the
pH value of CG2 was almost neutral as it was free of any trace of catalyst compared
to CG1. This was also attributed to the fact that CG2 was produced from the
transesterification reaction using 15% KOH/Al2O3 catalyst
that could be easily separated by filtration after the reaction process.
It could also be deducted from Table 3 that CG2 has nearly achieved the technical grade as that of PG based on the physical properties. Nevertheless, the moisture content of each CG1 and CG2 was slightly higher by a relative percentage of 20-35% than the PG moisture content. It was postulated that the small moisture content could be further reduced by ultrafiltration or membrane nanofiltration and it would be dealt with in the near future.
CONCLUSIONS
Purified glycerol of a considerable grade can be produced from the crude glycerol by-product of a transesterification process by a combination of 3 purification steps namely (1) neutralization process, (2) microfiltration and (3) ion exchange resins chromatography methods. Crude glycerol (CG2) as a product of the transesterification palm oil with heterogeneous catalyst was free from catalyst and relatively easier to be separated than the crude glycerol (CG1) produced from transesterification over homogeneous catalyst. Consequently, the neutralization of CG2 required less than 50% of the amount of phosphoric acid to that of CG1 to reach pH 7. In addition, a lower weight amount of Amberlite ion exchange resins were needed to sufficiently adsorb and exchange free cations and anions from the salts formed during the neutralization of CG2 sample. HPLC and FTIR analyses were carried out to check on the purity level of the samples. Both types were free from any impurities as only glycerol peaks and bands were detected at the end of the purification process. A few physical property tests were also conducted to assess the quality of the purified CG1 and CG2 to be compared to that of a commercial Pure Glycerol (PG). It was found that the viscosity, pH value, free fatty acid value and moisture content of CG1 and CG2 were not that dissimilar to the PG properties. Nevertheless, CG2 has achieved the nearest physical properties values to PG making it the better product of the two crude glycerol samples studied in this research.
ACKNOWLEDGMENT
The authors wish to thank National University of Malaysia (UKM) for funding this project under research grant code UKM-GUP-BTK-08-14-306.
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