The xylan recovered from alkaline black liquor (ABL) of oil palm frond (OPF) has the potential to be converted into value-added products that hold promise, especially for the pharmaceutical industry. This research highlights the maximum xylan relative recovery extracted from ABL by varying the extraction parameters such as the concentration of sodium hydroxide (NaOH) (2 to 10%) (w/v), reaction temperature (60 to 140 °C), and extraction time (30 to 150 min), followed by a 2-stage precipitation method. 6 M of hydrochloric acid (HCl) was used in the first stage to separate the lignin sub-fraction (LF) from the ABL, and 95% ethanol was used in the second stage to obtain xylan sub-fraction (XF). The optimal condition of 6% NaOH (w/v), 100 °C, and 60 min was able to recover 84% of xylan, with low contamination of lignin (7.7%) and glucan (0.3%) in XF, while higher contamination of lignin (19.3%) and glucan (10.9%) with lower amount of xylan (8.8%) were found in LF. The amount of lignin and glucan in LF through the first precipitation was higher than in XF from the second precipitation, leaving remaining fraction of XF mainly composed of xylan. In sum, the developed process reduced the alkali consumption while retaining a high xylan recovery under mild process conditions.
Enhancement of High Xylan Recovery from Black Liquor of Alkaline Pretreated Oil Palm Frond and its Physicochemical Properties
Nur Syahirah Ahmad Sobri,a Shuhaida Harun,a,b,* Nor Shahirah Ishak,a Jamaliah Md Jahim,a,b and Abdul Wahab Mohammad a,b
The xylan recovered from alkaline black liquor (ABL) of oil palm frond (OPF) has the potential to be converted into value-added products that hold promise, especially for the pharmaceutical industry. This research highlights the maximum xylan relative recovery extracted from ABL by varying the extraction parameters such as the concentration of sodium hydroxide (NaOH) (2 to 10%) (w/v), reaction temperature (60 to 140 °C), and extraction time (30 to 150 min), followed by a 2-stage precipitation method. 6 M of hydrochloric acid (HCl) was used in the first stage to separate the lignin sub-fraction (LF) from the ABL, and 95% ethanol was used in the second stage to obtain xylan sub-fraction (XF). The optimal condition of 6% NaOH (w/v), 100 C, and 60 min was able to recover 84% of xylan, with low contamination of lignin (7.7%) and glucan (0.3%) in XF, while higher contamination of lignin (19.3%) and glucan (10.9%) with lower amount of xylan (8.8%) were found in LF. The amount of lignin and glucan in LF through the first precipitation was higher than in XF from the second precipitation, leaving remaining fraction of XF mainly composed of xylan. In sum, the developed process reduced the alkali consumption while retaining a high xylan recovery under mild process conditions.
Keywords: Sodium hydroxide; Xylan recovery; Oil palm frond; Alkaline extraction; Hemicellulose; Lignocellulose; Glucan recovery; Acid-insoluble lignin
Contact information: a: Centre for Sustainable Process Technology (CESPRO), Faculty of Engineering and Built Environment, Universiti Kebangsaan Malaysia, 43600 Bangi, Selangor, Malaysia; b: Chemical Engineering Programme, Faculty of Engineering and Built Environment, Universiti Kebangsaan Malaysia, 43600 Bangi, Selangor, Malaysia; *Corresponding author: email@example.com
The utilisation of lignocellulosic biomass (LCB) has been of growing interest for several decades in industrial processes, as it is the most propitious material for renewable energy and bio-based products. LCB is mainly composed of three polymers; cellulose, hemicellulose, and lignin together with small amounts of other components including acetyl groups, minerals, and phenolic substituents. As an equatorial nation, Malaysia can take advantage of the vast availability and systematic replantation program of the palm oil industry as one of the easiest supplies of lignocellulosic biomass. The palm oil industry is a key economic factor that generates a material effect to the agricultural sector, with 2.44 million tonnes of crude palm oil production every year (Sime Darby Plantation Sustainability Annual Report 2014). The abundant lignocellulosic biomasses produced from the oil palm industry are rich with various carbohydrate sugars and other useful chemical compounds (Shuit et al. 2009). In an unorganised development, such as intensive plantation activities, there may be damage to forest systems, changes in the landscapes’ flora and fauna, and extreme land pollution due to the application of pesticides and herbicides. Therefore, waste disposal is huge problem associated with the oil palm industry.
Palm oil trees wastes can be developed into various types of resources, for instance, bioenergy and other value-added products (Abdullah and Sulaiman 2013). Oil palm fronds (OPF) are agricultural wastes of the palm oil industry, and they are structurally lignocelluloses-based that contain cellulose and hemicelluloses (Fazilah et al. 2009). Oil palm fronds have been extensively utilised for the production of bio-based products and as a feedstock in biorefineries for conversion into a wide range of valuable products. Recently, oil palm fronds have been utilised in the manufacturing of activated carbon through pyrolysis (Maulina and Rahmadi 2017) and in the production of oxalic acid through oxidation (Maulina and Anwari 2018). Oil palm fronds are composed of 30.4% hemicellulose (Saleh et al. 2011), which is the second most prolific polysaccharide in nature, representing approximately 20 to 30% of lignocellulosic biomass (Ebringerová et al. 2008). Hemicellulose polymers are complex components found in the cell walls of plants. Hemicellulose forms hydrogen bonds and covalent bonds with cellulose and lignin, respectively. Many notable applications of hemicelluloses by-products have been discovered and industrialised such as xylans.
Xylan is the most abundantly occurring heterogeneous biomolecule present in the hemicelluloses, and it is a promising biomaterial for pharmaceutical as well as food and non-food applications. Xylans have been industrially converted into xylose, xylitol, furfural, and prebiotics (Peng et al. 2009). Xylitol can be manufactured through the hydrolysis of xylan, crystallisation of xylose, and hydrogenation, which has been established in a variety of food products (Ebringerová and Heinze 2000). For instance, xylans in the dietary fibre of cereals aid in decreasing blood cholesterol and reducing postprandial blood glucose and insulin response in humans and animals (Asp et al. 1993).
Different techniques of extracting xylan from different agricultural residues have been studied in order to find novel applications, as there has been a growing interest in the characterisation of xylan. The production of xylan from its source materials will differ as per the method of extraction used in addition to the linkages and hydrogen bonding of cellulose and lignin within it (Samanta et al. 2012). The crucial part in obtaining the xylan is its component in lignocelluloses that are bound tightly, which makes it onerous to separate the xylan from lignins (Sun et al. 2004). This is one of the main reasons why the material properties of xylan have not been industrially exploited. Extraction is needed to alter the structure of the lignocellulose and break down the linkages with other biomolecules within the material.
Various methods have been used to extract xylan from agricultural wastes, and the alkaline extraction method is the most widely used, as it is the most promising method to accomplish complete utilisation of lignocelluloses (Ryberg et al. 2011). A large number of hemicelluloses containing xylan and partial lignin fractions with low molecular weight are degraded and dissolved into the black liquor generated after the extraction process, but many past studies focused on maintaining cellulose content for the production of value-added product. Relatively, less attention has been paid to the black liquor, and it is usually disposed as wastewater, which impacts to the environment.
The isolation of xylan in aqueous media occurs by the hydrolysis of ester linkages between hemicellulose and other components in an alkaline solution (Zulyadi et al. 2016). Alkaline black liquor contains xylan and partial fractions of lignin, which requires two-stage precipitation, starting with the acidification of black liquor, followed by ethanol precipitation to obtain the fractions that contain mainly xylan. The acidification process precipitates 90% of lignin from the black liquor (Zhu and Theliander 2015). Xylan is the precipitate formed through the alkaline solubilisation and an addition of ethanol, since cellulose cannot be dissolved in sodium hydroxide nor potassium hydroxide and it is observed that alcohol would not precipitate lignin (Samanta et al. 2012). Usually, the isolation of hemicellulose is done by using alkaline solution such as sodium hydroxide (NaOH) for softwood and potassium hydroxide (KOH) for hardwood (Peng et al. 2011).
There is limited information regarding the optimum condition of the alkali extraction to raise the recovery of xylan. This study highlights the maximum recovery of xylan extracted from the black liquor of alkaline pretreated OPF by varying the parameters of extraction such as alkaline concentration, temperature, and extraction time. This process was followed by the two-stage precipitation method using 6 M HCl and 95% ethanol to obtain the fractions namely lignin sub-fraction (LF) and xylan sub-fraction (XF), respectively. The maximum xylan percentage relative recovery was investigated, and the chemical composition and physicochemical properties of these fractions were examined by sugar analysis, acid-insoluble lignin (AIL), and Fourier transform infrared (FT-IR).
Preparation of oil palm frond bagasse
The petioles of OPF were collected from the oil palm tree (Elaeis guineensis) plantation at Universiti Kebangsaan Malaysia, Bangi, Selangor, Malaysia on September 2018. The petioles were freshly cut about the average length of 1 to 3 m, and the material was processed on the same day to keep assure of its freshness. The OPF juice was removed by pressing in a sugarcane presser machine model SCM (6.5 hp petrol-driven). The OPF bagasse was dried under sun for 72 h until the moisture content dropped to less than 10%, as measured by a moisture analyser (IR35M, Denver Instrument, New York, NY, USA). After the drying, the OPF was ground to 2 mm particle size using a grinder (Fritsch, Idar-Oberstein, Germany) and sieved through 0.5 mm mesh for the removal of particles in powdered form resulting from the grinding process. The ground samples were sealed in a plastic bag and stored at 4 C. Prior to the optimisation and characterisation studies, the samples were oven-dried at 45 C until the moisture content reached ≤10 %.
The chemical analysis of raw OPF was conducted by following the methods developed by the National Renewable Energy Laboratory (NREL) which include the determination of total extractives, structural carbohydrates, lignin, and ash content (Hames et al. 2008; Sluiter et al. 2008a,b, 2012). In the early stages, the native OPF underwent the water extraction process, followed by ethanol extraction using the accelerated solvent extraction ASE 350 (ASE-Dionex, Sunnyvale, CA, USA) to remove the extractive compounds. Approximately 0.3 g of extractive-free OPF was further subjected to two-step acid hydrolysis process using 3 mL of 72% sulphuric acid at 30 C for 60 min, followed by dilution using 84 mL of deionised water at 121 C for 60 min to quantify the structural carbohydrates content. The methods developed by NREL helped in determining the chemical composition of raw biomass feedstocks for biomass conversion processes.
Fig. 1. Scheme for sequential extraction of xylan from OPF
Optimization run of xylan extraction
The scheme for sequential extraction of xylan from OPF was illustrated as can be seen in Fig. 1. Optimization run (OR) of xylan extraction was initially investigated by varying the concentration of NaOH, temperature, and extraction time to optimise the alkaline extraction conditions for maximum xylan relative recovery. Various concentrations of NaOH solution (2, 4, 6, 8, and 10%) (w/v), temperatures (60, 80, 100, 120, and 140 C), and extraction time (30, 60, 90, 120, and 150 min) were evaluated upon soaking the OPF with the ratio of 1:10 (solid to liquid). The black liquor was collected after the extraction process and was further subjected to acidification by 6 M hydrochloric acid (HCl) until it reached pH 5.5. The acidified black liquor was brought for centrifugation at 10000 rpm for 15 min. The precipitate formed, namely the lignin sub-fraction (LF), was filtered and freeze-dried using Martin Christ Alpha 1-4 LSC freeze-dryer until constant weight was achieved. The supernatant from the precipitation of LF was added with 3 volumes of 95% (v/v) ethanol until it became saturated for about 10 min. The mixture was brought for centrifugation again for 15 min at 10000 rpm. The precipitate formed, the xylan sub-fraction (XF), was freeze-dried after filtration until the weight became constant. Xylan obtained in the form of pellet (LF and XF) was used as xylan source and stored at room temperature for further analyses and characterisations while the supernatant was kept for sugar analysis. The following formula (Eqs. 1, 2, and 3) were used to calculate the relative recovery of xylan, glucan, and lignin, respectively, after the extraction,
Verification run of xylan extraction under optimized condition
The optimization run (OR) was performed by using one-factor-at-a-time (OFAT) method, and the concentration of NaOH, temperature and time were varied to obtain the maximum xylan relative recovery. In order to ensure the accuracy of the data obtained from OR, triplicates of each verification run (VR1, VR2, and VR3) were further carried out under the optimal condition obtained from OR with the ratio of 1:10 (solid to liquid). The relative recovery values of xylan, glucan and lignin obtained from VR were calculated based on the Eqs. 1, 2, and 3, respectively.
Determination of acid-insoluble lignin content
The lignin content in OPF bagasse, LF, and XF was measured by acid-insoluble lignin (AIL), which was determined after a two-step hydrolysis process with 72% and 4% sulphuric acid, as previously described (Sluiter et al. 2012). Approximately 3 mL of 72% H2SO4 was added to 0.3 g of each fraction, and the mixtures were incubated at 30 °C for 60 min. Subsequently, 84 mL of deionised water was added to the mixtures, which were autoclaved at 121 °C (1.03 × 105 Pa) for 60 min. The filter was pre-weighed to be used for filtering off the lignin. The filtered hydrolysate was analysed for sugar content, while the residues were placed in a desiccator before being weighed. The AIL content was obtained from the percentage of weight loss.
Sugar composition and phenolic acid of extracted xylan
Hydrolysis of LF and XF fractions using sulphuric acid (H2SO4) was performed to determine their sugar composition and phenolic acid. The sugar composition was quantified using high performance liquid chromatography (HPLC) (UltiMate 3000 LC system, Dionex, Sunnyvale, CA, USA) detected by a refractive index (RI) detector (RefractoMax 520, ERC, Buchholz, Germany) set at 40 °C by using Rezex ROA-Organic Acid H+ column (300 mm × 7.8 mm; Phenomenex, Torrance, CA, USA), with a guard column (50 mm × 7.8 mm). The column temperature was maintained at 60 °C, and 0.005 N H2SO4 was isocratically eluted at a flow rate of 0.6 mL/min with the sample injection volume set at 20 µL. Concentrations of ferulic acid and coumaric acid were also analysed by using Agilent 1100 HPLC system (California, USA) detected by ultraviolet-diode array detector (UV-DAD) set at 220 nm by using Gemini C-18 column (Phenomenex, Torrance, CA, USA). The column temperature was set at 40 °C, and 20 mM sulphuric acid/ acetonitrile (1:10) was isocratically eluted at a flow rate of 0.8 mL/min with the sample injection volume set at 20 µL. Each of the mobile phase was initially vacuum filtered and degassed.
Fourier transform infrared spectroscopy (FTIR) analysis
The infrared spectra of OPF bagasse, extracted fractions (LF and XF), and commercial beechwood xylan were carried out using a Nicolet 6700 FTIR spectrophotometer (Thermo Fisher Scientific, MA, USA) with the attenuated total reflectance (ATR) method in the frequency range of 4000 to 400 cm⁻1 with resolution of 4 cm⁻1 to analyse the changes in functional groups in the xylan fractions.
RESULTS AND DISCUSSION
Compositional Analysis of Oil Palm Frond (OPF) Bagasse
The potential of an agricultural residual as a feedstock for biorefinery processes was initially predicted based on its chemical composition to attain a dependable and comparable compositional analysis of OPF, as it allows the biomass’ economical potential in biochemical industries to serve as a feedstock (Tan et al. 2016). The composition of OPF obtained in this study and by other researchers is shown in Table 1.
Table 1. Comparative View of Compositional Analysis of Raw OPF with Other Researchers
In this study, glucan was the major structural carbohydrate in OPF bagasse, at 34.7 ± 4.2%, followed by xylan, 19.4 ± 3.8%. Hence, the total structural carbohydrates content in OPF bagasse was 54.1 ± 7.9%. The results were similar with other studies in which glucan and xylan are the major structural carbohydrates present in OPF bagasse (Fauzi et al. 2016; Luthfi et al. 2016; Tan et al. 2016; Manaf et al. 2018). However, the total structural carbohydrates in this study was slightly lower than in others (Table 1). The variations in the source of OPF, maturity of the plant, and the conditions of weather might contribute to these differences. Because OPF was rich in xylan, the extraction of xylan from OPF was continued for further analyses. The total lignin content was 20.7 ± 0.5%. Lignin is also one of the major building blocks in lignocellulosic biomass; therefore, it is important to determine the total lignin percentage in the raw sample to enhance the effectiveness of the overall process. The content of total structural carbohydrates especially xylan proves that the OPF has the potential to be used as a feedstock in biorefineries for the production of value-added products.
Optimization Run (OR) of Xylan Extraction
During alkaline extraction, black liquor was generated after treating the ground OPF bagasse (Fig. 2a) with NaOH (Fig. 2b). The pH remained relatively constant but slightly decreased due to consumption of OH⁻ as hemicellulose and lignin were solubilised. An intense colour change took place from black (Fig. 3a) to yellowish orange (Fig. 3b) during the acidification of black liquor with 6 M HCl as the pH was lowered from 13.0 to 5.5. During the precipitation using ethanol to extract xylan sub-fraction (XF), two layers were formed (Fig. 3c). The extract was centrifuged, and the precipitated xylan was freeze-dried for 16 h before being weighed and powdered (Fig. 4). The recovery of xylan from OPF was calculated using Eq. 1, and it was observed based on different concentrations, temperatures and extraction time. Henceforth, xylan extraction was carried out in bulk for subsequent analysis after obtaining the best levels of alkali and its condition. Xylan recovery for XF, which was after the precipitation with ethanol, resulted in high recovery of xylan as compared to LF.
Fig. 2. (a) Untreated OPF bagasse after grinding process, extraction of OPF bagasse soaked in NaOH (b) before extraction, and (c) after extraction
In these alkaline processes, xylan and lignin components were solubilised into the aqueous alkaline black liquor by the peeling reaction and nucleophilic substitution. The pH of the black liquor remained relatively constant but slightly decreased due to consumption of OH⁻ as xylan and lignin were solubilised. In order to obtain pure xylan precipitate, the lignin in the black liquor must be precipitated out via acidification process by lowering the pH of black liquor. The xylan precipitate (XF) was then obtained via the ethanol precipitation from the acidified black liquor. The precipitation of lignin from black liquor by acidification occurs because of the protonation of ionised phenolic groups on lignin molecules. The protonation of phenolic groups reduces the electrostatic repulsive forces between lignin molecules, which then become less hydrophilic, leading to precipitation; lignin sub-fraction (LF) and the remaining liquid was poured into ethanol to precipitate out the xylan sub-fraction (XF) (Zhu and Theliander 2015). The two stages of precipitation defined the different molecular weight of hemicellulose, in which hemicellulose with higher molecular weight was usually obtained from the first precipitation using acid, while the hemicellulose with lower molecular weight was obtained from the second stage of precipitation using ethanol (Nacos et al. 2006).
Fig. 3. (a) Alkaline black liquor obtained after extraction process, (b) changes in colour during pH change, (c) formation of 2 layers after ethanol precipitation, (d) precipitated xylan formed by centrifugation
Fig. 4. Xylan fractions obtained after (a) acidic precipitation; LF and (b) ethanol precipitation; XF
Effect of concentration of NaOH on the xylan relative recovery
To investigate the effect of NaOH concentration on xylan relative recovery, different NaOH concentrations (2, 4, 6, 8, and 10%) (w/v) were used at a fixed time (60 min) and temperature (100 C). Ester linkages formed in the lignocellulosic matrix of biomass was initially hydrolysed by alkaline before being extracted into alkaline medium. These are the two processes involved to extract the xylan from lignocellulosic biomass (Doner and Hicks 1997; Peng et al. 2010). Hemicellulose polysaccharides were isolated in substantial amounts under alkaline extraction, which showed that it was the most efficient method. After the extraction took place, a moiety of hemicellulose material was brought into solution due to the swelling of cellulose, hemicelluloses, and celluloses by hydroxyl ions (Sun et al. 2005). Based on Table 2, the recovery of xylan for both LF and XF were increased from 10.6 ± 0.3% to 22.6 ± 0.3% and 23.3 ± 0.1% to 64.7 ± 0.7%, respectively, at 2% (w/v) to 6% (w/v). However, as the concentration was getting higher, the xylan relative recovery for LF and XF started to decrease from 18.9 ± 0.3% to 17.8 ± 0.1% and 53.9 ± 0.5% to 47.1 ± 0.4%, respectively, at 8% (w/v) to 10% (w/v). The relative recovery of all xylan fractions decreased at higher concentrations, indicating that appreciable amounts of xylans were leached out (Nasir and Saleh 2016). This also indicates that mild conditions were the best for xylan extraction. The highest xylan recovered of 22.6 ± 0.3% for LF and 64.7 ± 0.7% for XF were obtained at 6% NaOH (w/v); hence, it was chosen for further analysis.
Effect of temperature on the xylan relative recovery
The effects of different temperatures (60, 80, 100, 120, and 140 C) were studied at fixed parameters of 6% NaOH (w/v) and 60 min. According to Table 2, the xylan relative recovery for LF and XF increased from 17.4 ± 0.4% to 25.4 ± 0.4% and 39.0 ± 0.3% to 66.8 ± 0.2%, respectively, at 60C to 100 C, but it decreased from 22.5 ± 0.4% to 20.2 ± 0.3% for LF and 62.4 ± 0.9% to 46.9 ± 0.5% for XF at 120 C to 140 C. Warm alkaline solutions enhance hemicellulose degradation, but in cold alkaline solutions, hemicellulose has a finite solubility of (Nasir and Saleh 2016). The highest xylan relative recovery obtained for LF and XF was 25.4 ± 0.4% and 66.8 ± 0.2%, respectively, at 100 C. Thus, high temperature is needed in extracting the xylan to promote penetrating the lignified cell wall (Mosier et al. 2005). However, at higher temperatures, the decreased xylan recovery may be due to the degradation of hemicellulose by end-wise peeling reactions (Höije et al. 2005). High temperature caused the cleavage of linkages between the glycosyl units, which led to minor degradation (Bian et al. 2012). Therefore, a reaction temperature of 100 C was chosen as optimum temperature for further analysis.
Effect of extraction time on the xylan relative recovery
The effects of different extraction times (30, 60, 90, 120, and 150 min) on xylan relative recovery during alkaline extraction were examined after an optimum concentration and temperature were obtained at 6% NaOH (w/v) and 100 C, respectively. As can be observed from Table 2, the xylan recovery for LF and XF were increased from 7.4 ± 0.5% to 8.8 ± 0.4% and 54.1 ± 0.2% to 84.0 ± 0.1%, respectively, at an extraction time of 30 to 60 min. However, the xylan recovery dropped from 8.3 ± 0.7% to 7.7 ± 0.6% for LF and 62.6 ± 0.3% to 43.8 ± 0.3% for XF at the longer extraction time of 90 to 150 min.
Table 2. Optimization Run (OR) of Xylan Extraction for Percentage Relative Recovery of Xylan, Glucan, and Lignin in Alkaline Black Liquor, Lignin, and Xylan Fractions Under Varying Operating Conditions
The results indicated that increasing the extraction time may escalate the recovery of xylan, as previously noted (Saleh et al. 2012; Nasir and Saleh 2016). Hydrolytic cleavage may degrade polysaccharides and induce changes in the polysaccharide molecule structure at elevated time (Azhar et al. 2015). However, the change in polysaccharide molecule structure was induced due to extended time of extraction (Cai et al. 2008). In sum, the optimal conditions for xylan extraction from OPF were a NaOH concentration at 6% (w/v) and temperature of 100 C for 60 min with a dry OPF-to-NaOH ratio of 1:10 (g/L).
Fig. 5. Comparative view of xylan, glucan and lignin yield in raw OPF, lignin sub-fraction (LF) and xylan sub-fraction (XF) from OR obtained under optimal condition of 6 % NaOH (w/v), 100 (C) and 60 min.
The xylan relative recovery of each condition performed was higher in XF as compared to LF. However, the results for glucan and lignin relative recovery were found to be higher in LF rather than XF. Based on the results obtained under optimal condition of 6% NaOH (w/v), 100 C and 60 min, greater lignin recovery of 19.3 ± 0.1% was observed compared to 10.9 ± 0.1% of glucan in LF. The trend was also similar in XF where lignin (7.7 ± 0.2%) was higher than glucan (0.3 ± 0.3%). The relative recovery of glucan was very low, which indicated that significant amount of glucan was unhydrolyzed in the black liquor, as it was retained in the alkaline pretreated OPF. Also, the amount of lignin in LF after acidification process was higher than XF, leaving remaining fraction of XF mainly composed of xylan. According to Fig. 5, the result of xylan yield calculated from Eq. 4 showed an increase from 1.7 ± 0.1% to 16.3 ± 0.1% in LF and XF, respectively. These values corresponded to increase in the relative recovery of xylan from 8.8 ± 0.4% to 84.0 ± 0.1% in LF and XF, respectively. This could explain that the optimal condition obtained in this study provides high xylan recovery of 84 ± 0.1% with low contamination of lignin (7.7 ± 0.2%) and glucan (0.3 ± 0.3%).
Verification Run (VR) of Xylan Extraction Under Optimized Condition
The main objective of this study was to evaluate the factors influencing the maximum amount of xylan that could be recovered from the black liquor. An optimization run (OR) of xylan extraction was performed by using a one-factor-at-a-time (OFAT) method, and the results showed that 8.8 ± 0.4% and 84 ± 0.1% of xylan was successfully recovered in LF and XF, respectively. Three variables, namely NaOH concentration, temperature, and time, were the main factors affecting the xylan recovery. The verification was run under the optimal conditions of 6% NaOH (w/v), 100 C and 60 min, and the results are given in Table 3. The average results of xylan recovered from verification run (VR1, VR2 and VR3) in LF and XF were 8.5 ± 0.3% and 83.3 ± 0.6%, respectively, which is very close to the results obtained from OR. Hence, the consistency of the results showed that the optimal condition was able to provide maximum recovery of xylan from black liquor, preserving the xylan polymeric form.
Table 3. Comparative View of Optimization Run (OR) and Verification Run (VR) of Xylan Extraction based on Percentage Relative Recovery under Optimized Condition
Composition of Lignin Sub-Fraction (LF) and Xylan Sub-Fraction (XF)
Sugar composition of LF and XF
The sugar composition of extracted xylan varies, depending on the isolation method used and the type of raw materials used during the process (Peng et al. 2009). Various different sugar substituents such as glucose, arabinose, mannose, or acidic groups such as acetic and uronic acid attached to the xylose backbone describes the heterogeneity of xylan. According to Table 4, xylose was the predominant monosaccharide in XF, which contained of 18.5 ± 0.1% and 1.9 ± 0.1% of xylose in LF. Apart from xylose, glucose was found at a slight amount of 0.1 ± 0.1% in XF and 4.2 ± 0.2% in LF. This result is in accordance with other research findings in which xylose was predominantly found with a moderate amount of glucose in hemicelluloses of Indian wheat (Revanappa et al. 2007). Other monomers such as arabinose were not found in either fraction of xylan, which may be due to the decomposition of arabinose. During the solubilisation and hy