Independent variables and their levels for central composite design in optimization of alkaline delignification of steam-exploded pulp
The inevitable depletion of the world’s petroleum supply and the increasing problem of greenhouse gas effects have resulted in an increasing worldwide interest in alternative nonpetroleum-base source of energy. As the transportation sector is practically entirely depending on oil and as it is responsible for half of the total CO2 emission , the increasing in market share of renewable biofuels includes ethanol fuel. The uses of ethanol fuel will significantly reduce net carbon dioxide emission once it replaces fossil fuels because fermentation-derived ethanol is already a part of the global carbon cycle. However, to enhance the market position of the biofuel the production cost should be reduced. Nowadays, the raw material and enzyme production are the two main contributors to the overall costs, thus using high cellulose containing agricultural residues as feedstock agricultural could result in cost reduction. The techniques employed to produce bioethanol from agricultural residue materials or lignocellulosic materials are subjected to the same economical demands as the more traditional sugar and starch processes, as the price of bioethanol must be competitive with that of petrol. Conversion of lignocellulosic materials to monomeric sugars and finally ethanol must thus be performed at low cost, while still achieving high yields. This can be done by developing processes that require limited amounts of the material chemicals, yeast and enzymes. To convert lignocellulosic materials to monomeric sugars, they must pretreat by different methods, such as dilute acid, steam explosion, ammonia fiber explosion (AFEX) and dilute alkali. All of these methods can change lignocellulosic structure and enhance the enzymatic saccharification of cellulose to hexose sugar.
The bioconversion process from lignocellulose biomass to ethanol consists basically of three steps: pre-treatment, enzymatic hydrolysis and fermentation. Pretreatment is a necessary step to facilitate the enzymatic attack of lignocellulosic materials. Steam explosion is recognized as an efficient pre-treatment method in ethanol production . The raw material is treated at high pressure steam followed by suddenly rapid reduction in pressure resulting in substantial breakdown of the lignocellulosic structure, hydrolysis of the hemicellulosic fraction, depolymerization of the lignin components and defibration . Therefore, the accessibility of the cellulose components to degrade by enzymes is greatly increased. The process of ethanol production from lignocellulosic material is shown in Figure 1.
Numerous experimental studies of ethanol production from biomass have been carried out. A review article by Kaur
1.1. Response Surface Methodology (RSM)
Response surface methodology is an empirical statistical technique employed for multiple regressions analysis by using quantitative data. It solves multivariable data which is obtained from properly designed experiments to solve multivariable equation simultaneously. The graphical representation of their function was called response surface, which is used to describe the individual and cumulative effect of the test variables and their subsequent effect on the response. The effect of the variables on the response is investigated using second-order polynomial regression equation. This equation, derived using RSM for the evaluation of the response variables, is as follows:
Where Y is the response, bo, b, bii and bij are regression coefficients for intercept, linear, quadratic and interaction terms, respectively. The xi and xij are uncoded values for independent variables. An analysis of variance (ANOVA) is performed to determine the lack of fit and the effect of linear, quadratic and interaction terms on the response. Many researches have used RSM in optimization process as these examples. Roberto
1.2. Oil palm trunk
The oil palm tree (Elaeis guineensis) is indigenous to the tropical forests in weat Africa. The oil palm tree has become one of the most valuable commercial cash a crop due to the palm oil is used as a raw material in many industries such as soap, cosmetic, detergent, vegeTable oil and biodiesel. Nowaday almost 80% of the world oil palm plantation is centered at Southeast Asia, with most of it occurring in Indonesia (5.44 x 106 hectares) and Malaysia (4.85 x 106 hectares). Additionally, there are 260,000 hectares planted in Thailand, with smaller areas in the Philippines and some recent planting in Cambodia and Myanmar . Oil palm trunks are available only when the economic lifespan of the palm is reach at the time of replanting. The average age of replanting is approximately 25 years. The main economic criteria for felling are the height of the palm, reaching 13 m or above and the diameter of the felled trunk is around 45 cm to 65 cm. More than 15 million tons of oil palm trunks per year are replanted in the world . The increase of oil palm trunk every year can create massive pollutions thus development technology for value-added products are need for this raw material. There are many need uses of potential value-added products made from oil palm trunk such as particleboard, laminated board, plywood, fiberboard and furniture . Oil palm trunk can also be used for making paper . It can also be used as raw material in ethanol production, too .
The objectives of this research are performed according to central composite design (CCD) and response surface methodology (RSM) to optimize and compare the condition for delignification and hydrolysis of steam-exploded oil palm trunk prior to ethanol fermentation to understand the relationship between the critical factor involved in enzymatic degradation of pulp and conversion to ethanol.
2. Materials and methods
2.1. Raw material and microorganism
The steam-exploded pulp obtained from oil palm trunk was prepared by steam explosion treatment. An amount of 150 g of dry oil palm trunk chip sample was placed in 2.5 L batch digester (Nitto Koatsu Company, Japan). Heating was accomplished by direct steam injection into the digester and the temperature of steam at 214°C for 2 min. This condition was previous work by Punsuvon
Saccharomyces cervisiae TIRS 5339 obtained from TISTR, Thailand was used in this study. It was maintained on a medium containing 20.0 g/l glucose, 20.0 g/l peptone and 10.0 g/l yeast extract at 4ºC and subcultured every month at 30ºC. The growth medium of the yeast consisted of 10.0 g/l yeast extract, 6.4 g/l urea, 2.0 g/l KH2PO4, 1.0 g/l MgSO4-7H2O and 2.0 g/l glucose at pH 5.5 .
2.2. Alkaline delignification of steam-exploded pulp
The water-insoluble cellulose pulp obtained from steam explosion was delignified with potassium hydroxide. The reactions were carried out in a beaker under various maintained temperature. Before RSM was applied on alkaline delignification, approximate conditions for glucose content in pulps, namely concentration of pulp, concentration of alkaline solution, reaction time and temperature were determined by varying one factor at time while keeping the other constant. The initial step of the preliminary experiment was to select an appropriate amount of concentration of pulp. Five different concentrations of pulp (3, 6, 9, 12, 15 %w/v) were examined. The other three factors, concentration of alkaline solution, reaction time and temperature, were kept constant at 20%w/w, 60 min and 80ºC, respectively. Based on the glucose content in pulp after delignification, the optimum concentration of pulp was chosen. The second step of the preliminary experiment was to determine the concentration of alkaline solution. The glucose content in pulp was analyzed using the optimum condition of pulp chosen in the previous step. The alkaline solution concentration varied from 2 to 30% w/w while holding reaction time and temperature at 60 min and 80ºC. The third step of the preliminary experiment was to determine the reaction time. Using the concentration of pulp, concentration of alkaline solution, reaction time from the previous steps, alkaline delignification was studied under various reaction times from 15 to 90 min. The final step was to select an appropriate temperature by using the concentration of pulp, concentration of alkaline solution, reaction time from the previous step. The temperature varied from 30 to 100ºC. Based on these results the five level of each process variable were determined for RSM. The independent variables of RSM experiments were shown in Table1. Delignified pulp was recovered by filtration, washed several times with distilled water, died and then analyzed for glucose content. These pulps were ready to be used as the substrate for enzymatic hydrolysis.
2.3. Enzyme hydrolysis
Delignified pulps were hydrolyzed by cellulase (Celluclast 1.2L, Novozymes A/S Denmark) in flasks. The hydrolysis was performed in 0.05M sodium citrate buffer (pH 4.8) at 150 rpm of shaking. The dependent variables of experiments were shown in Table 2. All enzymatic hydrolysis liquor was analyzed for glucose content by High Performance Liquid Chromatography (HPLC).
2.4. Inoculums and ethanol fermentation
S. cerevisaie was initiated in the maintenance medium at 30ºC. The yeast was grown for 48 h at 170 rpm on a rotary shaker at 30°C. A 2.5 % w/v inoculums was used for subsequent subcultures. Ethanol fermentation was evaluated at 30°C in 150–ml Erlenmeyer flasks containing 100 ml fermentation media. The yeast fermentation medium consisted of the hydrolysis liquor containing 50g/l glucose, 2.0 g/l KHPO4, 1.0 g/l MgSO4.7H2O, 10.0 g/l yeast extracts and 6.4 g/l urea at pH 5.5. The flasks were sealed with a one-hole rubber stopper, which a glass tube was connected to an air lock filled with 40% sulfuric acid solution. Ethanol content from fermentation was analyzed by Gas Chromatography (GC).
|Concentration of pulp, %w/v||X1||3||6||8||12||15|
|Concentration of alkaline solution, %w/w||X2||2||8||14||20||26|
|Reaction time, min||X3||15||30||45||60||75|
|Reaction time, h||X1||10||30||50||70||90|
|Enzyme loading, Filter Paper Unit (FPU)/g substrate||X3||5||30||55||80||105|
|Concentration of pulp, %w/v||X4||1||2||3||4||5|
2.5. Experimental design
A central composite design was employed the response, namely percentage of glucose for alkaline delignification, and percentage of glucose yield for enzyme hydrolysis. The independent variables of alkaline delignification were X1, X2, X3 and X4 representing concentration of pulp, %w/v, and concentration of alkaline solution, % w/w, reaction time, min and temperature, °C, respectively. The independent variables of enzyme hydrolysis were X1, X2, X3 and X4 representing reaction time, h, temperature, °C, enzyme loading, FPU/g substrate and concentration of pulp, %w/v, respectively. Each variable to be optimized was coded at five levels: - α, -1, 0, +1 and + α. This gives a range of these variables of alkaline delignification (Table 1) and enzyme hydrolysis (Table2). Six replication runs at the centre (0, 0, 0) of the design were performed to allow the estimation of the pure error.
2.6. Statistical analysis
The data obtained by carrying out the experiment according to central composite design were analyzed by SPSS package (version 12.0). The response surface was expressed at the following second-order polynomial equation:
Where Y is the response (percent glucose, %), xi and xij are uncoded independent variables, bo is constant, bi is linear term coefficients, bii is quadratic term coefficients. bij is cross-product term coefficients. SPSS package was used for regression analysis of variance (ANOVA) and response surface methodology was performed using STATISTICA Software. Response surface plots were developed using the fitted second order polynomial equation obtain from regression analysis holding one of the independent variables at a constant value corresponding to the stationary point and changing the other two variables.
2.7. Glucose determination
The glucose content of hydrolysis liquid was analyzed by High Performance Liquid Chromatography (HPLC, Shimadzu, Kyoto, Japan) with refractive index detector. An AMINEX HPX- 87C carbohydrate analysis (Bio-Rad, Hercules, USA) was used as column. The mobile phase was deionied water with flow rate 0.6 ml/min. The injection volume was 20 μl and the column temperature was maintained at 80°C. The glucose content of the solid residue was determined based on monomer content that was measured after two steps of acid hydrolysis. The first step hydrolysis was performed with 72% (w/w) H2SO4 at 30ºC for 60 min. In the second step, the reaction mixture was diluted to 4% (w/w) H2SO4 with distilled water and subsequently autoclaved at 121°C for 1 h. This hydrolysis liquid was then analyzed for glucose content as described above. All analytical determinations were performed in duplication.
2.8. Ethanol determination
The ethanol content in fermented solution was analyzed by gas chromatography (GC). GC analysis was carried out with an Agilent Technologies (Santa clara, CA) 6890 gas chromatograph equipped with a flame ionization detector and a HP-5 (Bonded 5%phenyl, 95% dimethylpolysiloxane) capillary column (30 m x 0.32 mm ID, 0.25 μm film thickness). The temperature program was an initial temperature of 150ºC, increased to 190ºC at 10ºC/min then 15ºC/min to 250ºC, and held for 15 min. The injector and detector temperature were 250 ºC and 300ºC, respectively. Standard and sample were injected by using the split mode ratio of 50:1.
3. Results and discussion
3.1. Chemical components of oil palm trunk and steam exploded oil palm trunk pulp
The chemical components of steam exploded oil palm trunk pulp were 40.54% of cellulose, 9.36% of hemicelluloses, 38.46% of lignin and 8.56% of extractive in ethanol/benzene. This pulp obtained after steam explosion was used as raw material for optimization study in ethanol production.
3.2. Model fitting for optimization of alkaline delignification
The complete design matrix together with the values of both the experimental and predicted responses is given in Table3. Central composite design was used to develop correlation between the NaOH and KOH delignification variables to the percentages of glucose yield. The percentages of glucose yield were found to range between 41.4-49.8% for KOH delignification and 38.0-49.9% for NaOH delignification. Runs 17-23 at the center point were used to determine the experiment error. For both reponses of NaOH delignification and KOH delignification, the quadratic model was selected, as suggested by used software. The final empirical models in terms of coded factors are given by equation (1) and Equation (2) in Table 4. Where X1, X2, X2 and X4 were the coded values of test variables that represented pulp concentration, concentration of NaOH or concentration of KOH, reaction time and temperature, respectively. The variables X1X2, X1X3, X1X4, X2X3, X2X4 and X3X4 represented the interaction effects of pulp concentration and concentration of NaOH or concentration of KOH, pulp concentration and reaction time, pulp concentration and temperature, respectively. The quality of the model developed was evaluated based on the correlation coefficient R2. The R2 for the two obtained equations were found to be 0.875 and 0.890 in NaOH and KOH delignification, respectively. This indicates that 87.5% and 89.0% of the total variation in both delignifications were attributed to experimental variables studied. The R2 of 0.875 and 0.890 were considered as the good fit of the models.
The adequacy of the two models was further justified through analysis of variance (ANOVA). The ANOVA for the quadratic models for the two reponses is listed in Table 5. The Fisher’s test (F-test) carried out on experimental data make it possible to estimate the statistical significance of the proposed model. The F-test value of the models being 16.69 and 10.88, respectively for glucose in pulp obtained after NaOH and KOH lignifications, with a low probability value (p<0.01), we can conclude that they were statistically significant at 99.9% confidence level. It should be noted that p-value indicates the statistical significance of each parameter. It is based on hypothesis that a parameter is not significant, thus the more effect is significant. From Table 5, it was showed that the two models (both p-value<0.01) were adequate to predict the glucose in pulp obtained after NaOH and KOH lignifications within the range of studied variables.
Response surface contour plots of the RSM as a function of two factors at the time are helpful in understanding both the main and the interaction effects of these factors. The effects of concentration of pulp and concentration of NaOH on the percentage of glucose are shown in Figure 3 (a). Figure 3 showed that the concentration of pulp and NaOH could increased percent glucose in pulp after NaOH delignification. The concentration of pulp higher than 13.50% (w/w) had no significant effect on the amount of percent glucose in pulp. Response surface plot indicated the optimized condition at 12.50% w/v of pulp concentration and 21.50% (w/v) NaOH that gave 48.10% of percent glucose remained in pulp after NaOH delignification. Figure 3 (b) showed that increasing temperature and concentration of pulp could increased percent glucose in pulp after NaOH delignification. The temperature higher than 80ºC had no significant effect on the percent glucose in pulp after NaOH delignification. Response surface plot indicated the optimized condition at 12.5% w/w of pulp concentration and 80ºC that gave 47.95% of percent glucose remained in pulp after NaOH delignification. Figure 3 (c) showed that increasing time and concentration of pulp could increased percent glucose in pulp after NaOH delignification. The time longer than 67 min had no significant effect on the percent glucose in pulp after delignification. Response surface plot indicated the optimized condition at 12.5% w/v of pulp concentration and 65 min that gave 50.23% of percent glucose in pulp after NaOH delignification.
Response surface contour plots of the RSM on the effects of concentration of pulp and concentration of KOH on the percentage of glucose are shown in Figure 4 (a).Figure 4 (a) a showed that increasing concentration of pulp and KOH concentration could increased percent glucose in pulp. The pulp concentration higher than 12.5% (w/v) had no significant effect on percent glucose in pulp. Likewise, the KOH concentration higher than 23.4% (w/w) had no significant effect on percent glucose in pulp after KOH delignification. Response surface plot indicated the optimized condition at 10% (w/v) of pulp concentration and 23.5% (w/w) of KOH concentration that gave 49.04% of percent glucose in pulp after KOH delignification.
Figure 4 (b) showed that increasing concentration of pulp and temperature could increased percent glucose in pulp. The temperature higher than 80°C had no significant effect on percent glucose in pulp. Likewise, the concentration of pulp higher than 12% (w/v) had no significant effect on percent glucose in pulp after KOH delignification. Response surface plot indicated the optimized condition at 78°C of glucose in pulp after KOH delignification.
Figure 4 (c) showed that increasing time and concentration of pulp could increased percent glucose in pulp. The time longer than 60 min had no significant effect on percent glucose in pulp. Likewise, the concentration of pulp more than 12% (w/v) had no significant effect on percent glucose in pulp after KOH delignification. Response surface plot indicated the optimized condition at 12% (w/v) of pulp concentration and 70 min of reaction time that gave 48.35% of percent glucose in pulp after KOH delignification.
The summary result from combination of each response surface plot showed that the optimum condition for NaOH delignification was obtained from 11% (w/v) pulp concentration, 21% (w/w) NaOH concentration, 65 min reaction time and 78ºC temperature with the maximum glucose at 47.50% remaining in the pulp. The optimum condition for KOH delignification was 12% (w/v) pulp concentration, 23% (w/w) KOH concentration, 65 min of reaction time and 80ºC of temperature with the maximum glucose at 49.50% remaining in the pulp.
|37.112 - 0.166 X1 - 0.959X2 + 0.511X3 + 0.104X4 - 0.074X12
- 0.005X22 + 2.706X32 + 001X42 + 0.133X1X2 - 0.011X1X3 + 0.001X1X4 - 0.005X2X 3 - 0.005X2X4 - 0.006X3X4
|60.266 + 0.574X1 – 1.398X2 -0.320X3 + 0.091X4 – 0.030X12
- 0.001X22 + 0.006X32 – 002X42+ 0.133X1X2 – 0.008X1X3 + 0.006X1X4 - 0.004X2X 3 + 0.015X2X4 + 0.013X3X4
|Lack of fit||10||530.43||53.04||1.60||-|
|Lack of fit||10||523.45||52.34||1.01||-|
3.3. Model fitting for optimization of enzyme hydrolysis
The complete design matrix together with values of both experimental and predicted responses is given in Table 6. Central composite design was used to develop correclation between enzyme hydrolysis of both pulps obtained after NaOH or KOH delignification to percentage of glucose yield were found to range between 6.30-80.10% for pulp obtained after KOH delignification and 10.30-89.80% for pulp obtained after NaOH delignification. Runs 17-23 at the center point were used to determine the experiment error. For both responses of enzyme hydrolysis, the quadratic model was selected, as suggested by used software. The final empirical models in terms of coded factors are given by Equation (3) and Equation (4) in Table 7. Where X1, X2, X2 and X4 were the coded values of test variables reaction time, temperature, enzyme loading and pulp concentration, respectively. The variables X1X2, X1X3, X1X4, X2X3, X2X4 and X3X4 represented the interaction effects of reaction time and temperature, reaction time and enzyme loading, reaction time and pulp concentration, temperature and enzyme loading, temperature and pulp concentration and enzyme loading and pulp concentration, respectively. The quality of the model developed was evaluated based on the correlation coefficient R2. The R2 for the two obtained equations were found to be 0.867 and 0.935 in enzyme hydrolysis of pulp obtained after NaOH and KOH delignification. This indicated that 86.70% and 93.50% of total variation in both enzyme hydrolysis were attributed to the experimental variables studied. The R2 of 0.867 and 0.935 were considered as the good fit of the models.
The adequacy of the two models was further justified through analysis of variance as the same as delignification reaction in previous studied. The statistical result showed that the two models had p-values less than 0.01 that indicated these two models were adequate to predict the percentage of glucose yield in enzyme hydrolysis within the range of the studied variables.
In addition, response surface contour plots of the RSM on the effects of reaction time and concentration of pulp on the percentage of glucose in enzyme hydrolysis are shown in Figure 5 (a). Figure 5 (a) showed that increasing time and pulp concentration could increased percent glucose yield in hydrolyzed solution. The pulp concentration higher than 4.5% (w/v) had no significant effect on percent glucose yield in hydrolyzed in solution. Response surface plot indicated the optimized condition at 3% (w/v) of pulp concentration and 65 h of reaction time that gave 81.01% of percent glucose yield in hydrolyzed solution obtained after NaOH delignification. Figure 5 (b) showed that increasing time and temperature could increased percent glucose yield in hydrolyzed solution. The temperature higher than 50ºC had no significant effect on percent glucose yield in hydrolyzed solution. Response surface plot indicated the optimized condition at 44ºC of temperature and 65 h of reaction time that gave 81.33% of percent glucose yield hydrolyzed solution obtained after NaOH delignification. Figure 5 (c) showed that increasing time and enzyme loading could increased percent glucose yield in hydrolyzed solution. The enzyme loading higher than 65 (FPU/g substrate) had no significant effect on percent glucose yield in hydrolyzed solution. Response surface plot indicated the optimized condition at 54 (FPU/g substrate) of enzyme loading and 50 h of reaction time that gave 91.36% of percent glucose yield in hydrolyzed solution obtained after NaOH delignification. Figure 6 (a) showed that increasing time and pulp concentration could increased percent glucose yield in hydrolyzed solution. The reaction time longer than 75 h had no significant effect on percent glucose yield in hydrolyzed solution. Response surface plot indicated the optimized condition at 3% (w/v) of pulp concentration and 65 h of reaction time that gave 92.08% of percent glucose yield in hydrolyzed solution obtained after KOH delignification. Figure 6 (b) showed that increasing time and temperature could increased percent glucose yield in hydrolyzed solution. The temperature higher than 50ºC had no significant effect on percent glucose in hydrolyzed in solution. Response surface plot indicated the optimized condition at 50ºC of temperature and 65 h of reaction time that gave 88.91% (w/v) of percent glucose yield in hydrolyzed solution obtained after KOH delignification. Figure 6 (c) showed that increasing time and enzyme loading could increased percent glucose yield in hydrolyzed solution. The enzyme loading higher than 85 (FPU/g substrate) had no significant effect on percent glucose yield in hydrolyzed solution. Response surface plot indicated the optimized condition at 54.5 (FPU/g substrate) of enzyme loading and 66 h of reaction time that gave 88.44% of percent glucose yield in hydrolyzed in solution obtained after KOH delignification.
|Glucose yield (%)
|-49.956 + 2.654X1 + 20.429X2 + 1.310X3 - 6.477X4 - 0.021X12
- 0.228X22 - 0.012X32 - 1.134X42 - 0.005X1X2 + 0.001X1X3 + 0.003X1X4 + 0.002X2X 3 + 0.225X2X4 + 0.002X3X4
|Glucose yield (%)
|-51.956 + 2.654X1 + 20.332X2 + 1.410X3 - 6.477X4 - 0.021X12
- 0.224X22 - 0.012X32 - 1.835X42 - 0.004X1X2 + 0.001X1X3
+ 0.003X1X4 + 0.002X2X 3 + 0.225X2X4 + 0.003X3X4
The summary result from combination of each response surface plots showed that the optimum condition of enzyme hydrolysis for NaOH and KOH delignification were 54 FPU/g substrate, 65 FPU/g substrate enzyme concentation, 50 h, 60 h reaction time, 50ºC reaction temperature and 2.5% pulp concentration, respectively. The maximum glucose contents were 47.50% and 48.00% from NaOH and KOH delignification, respectively. The maximum glucose yield obtained were 85%, 81% and 75% from NaOH and KOH delignification and without delignification respectively. Both optimization conditions in enzyme hydrolysis of delignification pulp by NaOH and KOH used to hydrolyze undelignification pulp, the result showed that percent glucose yield was lower than those from delignified pulp about 8-10%.
3.4. Ethanol fermentation
3.4.1. Production of ethanol from pure glucose
S. Cerevisiae TISTR 5339 was grown in YMB containing 50 g/l glucose, 20 g/l peptone and 10 g/l yeast extract. The experiment was performed at room temperature. The result of ethanol production was shown in Table 7.
Table 8 showed the production of ethanol from 50 g/l of pure glucose by S. Cerevisiae TISTR 5339. The result showed that within 36 h of fermentation, the highest ethanol concentration was obtained at 21.92 g/l. The ethanol yield from calculation was 85.96%. This result indicated that S. Cerevisiae TISTR 5339 has 85.96% in capability to change pure glucose to ethanol.
3.4.2. Production of ethanol from hydrolyzed solution of NaOH and KOH delignified pulp and nondelignified pulp
The hydrolyzed solutions from three samples of pulp were concentrated to 50 g/l of glucose concentration. S. Cerevisiae TISTR 5339 was applied in the same amount as production of ethanol from pure glucose but pure glucose was replaced with the three hydrolyzed solutions. The fermentation solutions were analyzed by GC for ethanol concentration. The results were shown in Table 9.
Comparison of resulting ethanol after 36 h fermentation of NaOH and KOH delignified pulp was shown. The obtained ethanol concentration and yield from non delignified pulp was 16.25 g/l and 65%, respectively. The fermentation of KOH delignified gave ethanol concentration and yield at 16.42 g/l and 65.7% whereas those obtained from NaOH delignified pulp were 16.35 g/l and 65.4%, respectively. Alkaline delignification process showed no significant influence on the fermentation process. When the ethanol yield obtained from pure glucose and hydrolyzed solution (Table 8 and Table 9) were compared, it showed that the three hydrolyzed solutions gave lower ethanol yield due to the three hydrolyzed solution contained toxic substances such as furfural, 5-hydroxy methyl furfural, phenolic compound and acetic acid derived from steam explosion process. All substances can inhibit the fermentation of S. Cerevisiae TISTR 5339.
From this study on optimization of alkaline delignification and enzyme hydrolysis on steam exploded oil palm trunk followed by yeast fermentation to produce ethanol, an encouraging results were obtained. We concluded that delignification of steam explode pulp with NaOH was more influenced than delignification with KOH on term of less alkaline concentration consuming and lower reaction temperature. The comparison enzyme hydrolysis condition for both delignified pulp showed that NaOH delignified pulp gave higher the percentage of glucose yield than KOH delignified pulp. After optimizing the both delignification (NaOH and KOH) and both enzyme hydrolysis parameter by RSM, the highest ethanol yield of 65% were obtained from both fermentations with 50 g/l of glucose raw material.
The empirical quadratic models successfully predicted the percentage of glucose in pulp after delignification and the percentage of glucose in hydrolyzed solution after enzyme hydrolysis and they used in the development of better estimation tools. In addition, response surface plot in three-dimension obtained from the empirical quadratic models can show the interaction effect of two variables on the studied response and the optimum values of the selected variables are obtained from response surface plot, too.
AcknowledgmentsThe financial support for this work was provided by Centre of Excellence-Oil Palm Kasetsart University, Bangkok, Thailand.
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