- Open Access
Bioconversion of paper sludge to biofuel by simultaneous saccharification and fermentation using a cellulase of paper sludge origin and thermotolerant Saccharomyces cerevisiaeTJ14
© Prasetyo et al; licensee BioMed Central Ltd. 2011
- Received: 31 May 2011
- Accepted: 29 September 2011
- Published: 29 September 2011
Ethanol production from paper sludge (PS) by simultaneous saccharification and fermentation (SSF) is considered to be the most appropriate way to process PS, as it contains negligible lignin. In this study, SSF was conducted using a cellulase produced from PS by the hypercellulase producer, Acremonium cellulolyticus C-1 for PS saccharification, and a thermotolerant ethanol producer Saccharomyces cerevisiae TJ14 for ethanol production. Using cellulase of PS origin minimizes biofuel production costs, because the culture broth containing cellulase can be used directly.
When 50 g PS organic material (PSOM)/l was used in SSF, the ethanol yield based on PSOM was 23% (g ethanol/g PSOM) and was two times higher than that obtained by a separate hydrolysis and fermentation process. Cellulase activity throughout SSF remained at around 60% of the initial activity. When 50 to 150 g PSOM/l was used in SSF, the ethanol yield was 21% to 23% (g ethanol/g PSOM) at the 500 ml Erlenmeyer flask scale. Ethanol production and theoretical ethanol yield based on initial hexose was 40 g/l and 66.3% (g ethanol/g hexose) at 80 h, respectively, when 161 g/l of PSOM, 15 filter paper units (FPU)/g PSOM, and 20% inoculum were used for SSF, which was confirmed in the 2 l scale experiment. This indicates that PS is a good raw material for bioethanol production.
Ethanol concentration increased with increasing PSOM concentration. The ethanol yield was stable at PSOM concentrations of up to 150 g/l, but decreased at concentrations higher than 150 g/l because of mass transfer limitations. Based on a 2 l scale experiment, when 1,000 kg PS was used, 3,182 kFPU cellulase was produced from 134.7 kg PS. Produced cellulase was used for SSF with 865.3 kg PS and ethanol production was estimated to be 51.1 kg. Increasing the yeast inoculum or cellulase concentration did not significantly improve the ethanol yield or concentration.
- Ethanol Production
- Ethanol Concentration
- Ethanol Yield
- Cellulase Activity
Recently, much research has been conducted on reducing the input energy and cost of ethanol production. Around 5 million tons of paper sludge (PS) is discharged annually by the paper manufacturing industry in Japan. Disposing of PS in landfill or by incineration creates environmental problems, and legislative trends in many countries are restricting the amount and types of materials that are permitted to be disposed of by landfill . The production of bioethanol from PS can reduce dependence on fossil fuels while simultaneously solving the environmental problems associated with PS disposal. The use of bioethanol produced from PS offers an alternative source of energy, which could help overcome the current fossil fuel crisis and slow global warming. Using industrial waste materials as raw materials for bioethanol production is increasingly being researched [2, 3], due to the lower costs of raw materials and to avoid competition with human needs occurring when food crops are used, as is the case for first generation production processes.
Recent research into ethanol production from PS has been reported, using pretreatments such as mechanical grinding or phosphoric acid swelling to improve saccharification yield and efficiency . To remove hemicelluloses in the lignocellulosic material contained in recycled PS and cotton gin waste, mixing with steam treatment has been described as an effective pretreatment. However, this pretreatment method generated compounds that are toxic to the microorganism responsible for fermentation. Some inhibitors, such as furfural and hydroxymethylfurfural that are derivatives of lignin, significantly influence the performance of cellulase and ethanol fermentation by yeast [5, 6]. By using recycled PS that contains calcium carbonate (overliming), the toxic compounds can be eliminated . An advantage of PS as a carbon source over other lignocellulosic materials in bioethanol production is that pretreatment is not required, since most of the lignin has already been removed during the pulping that forms part of the paper manufacturing process.
The conventional yeast used in anaerobic alcohol fermentation releases 8.1 kJ/C mol glucose and cannot degrade xylose , which constitutes more than 10% of the reducing sugars (RS) contained in PS. When carrying out the process on an industrial scale, the bioreactor culture temperature must be controlled using cooling water. Using thermotolerant yeast reduces the costs involved in cooling the fermentation, as well as costs associated with the distillation of ethanol.
Ethanol concentration is an important factor of biofuel production, and should be at least 40 g/l in order to decrease the energy required during the ethanol separation and purification processes . In order to achieve ethanol concentrations of 40 g/l, research has been conducted into enabling ethanol production in semicontinuous fed-batch reactors. Starting ethanol concentrations of about 20 g/l have been reported, with the concentration reaching 40 g/l after 36 h . Solid-state fed-batch fermentation processes conducted in a rotary drum have been shown to be an alternative method, and the gas phase containing ethanol was collected as its condensate at -10°C .
Most ethanol production from cellulosic biomass has been conducted using commercial cellulases. However, the potential to use PS as a carbon source using a cellulase produced by Acremonium cellulolyticus has already been shown . This fresh cellulase, which was produced using PS as carbon source can be used directly to hydrolyse PS organic material (PSOM) that contains cellulose and hemicellulose. Only simple separation processes to remove insoluble materials such as clay and other biomass are required. In the present study, we established efficient bioethanol production using cellulase produced from PS and thermotolerant Saccharomyces cerevisiae TJ14 in a simple process without any pretreatment of PS. To allow for comparison, Solka Floc (SF), which is composed entirely of cellulose, was used in separate hydrolysis and fermentation (SHF) and simultaneous saccharification and fermentation (SSF) processes for ethanol production. The performance of the process was evaluated and optimized to achieve a high ethanol concentration from PS for use as a biofuel.
Chemical composition of representative paper sludge (PS) ash 
Composition (% w/w)
Composition of dry paper sludge (PS)
Amount (g/g dry PS)
A. Cellulolyticus C-1 (Ferm P-18508), which is a hypercellulase producer and a mutant of wild-type A. cellulolyticus Y-94, was provided by Tsukishima Kikai Co. Ltd. (Tokyo, Japan) . A. cellulolyticus produces a complex mixture of cellulases, mainly comprised of 4 β-glucosidases (EC 188.8.131.52) and 12 distinct endocellulase/carboxymethyl cellulase (CMCases, EC 184.108.40.206) [15, 16]. Other polysaccharide hydrolyzing enzymes, such as xylanases, amylases and β-1,3-glucanases, were also present . The most important enzyme in this mixture with regard to the current process is an endocellulose type III-A that can produce glucose from cellulose with no involvement of β-glucosidase .
A thermotolerant strain of S. cerevisiae, TJ14 , was used in this study. S. cerevisiae TJ14 is a hybrid strain between the heat-tolerant strain HB8(RI)-3A (MATahis3Δ1 leu2Δ0 ura3Δ0) and an ethanol producer yeast TISTR5056, generated by spore-to-cell mating. HB8 (RI)-3A is a derivative strain from a natural thermotolerant yeast isolate (C3723) found in Thailand and a thermosensitive laboratory yeast strain BY4742 (MATahis3Δ1 leu2Δ0 lys2Δ0 ura3Δ0) . S. cerevisiae TJ14 can be precultivated aerobically by shaking at 200 rpm .
Fermentation media and cultivations
The preculture medium for A. cellulolyticus consisted (per liter) of 40 g SF, 24 g of KH2PO4, 1 ml of Tween 80 (MP Biomedicals, Solon, OH, USA), 5 g of (NH4)2SO4, 4.7 g of K2C4H4O6·4H2O, 1.2 g of MgSO4·7H2O, 10 mg of ZnSO4·7H2O, 9.28 mg of MnSO4·7H2O, 8.74 mg of CuSO4·7H2O and 2 g of urea (pH 4.0). The medium was sterilized at 121°C for 20 min, with ZnSO4·7H2O, MnSO4·7H2O and CuSO4·7H2O sterilized separately. Urea was sterilized by filtering through a 0.45 μm filter membrane (Toyo Roshi Kaisha Co. Ltd., Tokyo, Japan). The cellulase production medium was comprised of 70 g PSOM/l as carbon source without the addition of any further minerals other than those contained in PS. KH2PO4 and urea were added at final concentrations of 10 g/l and 4 g/l, respectively. Cultures were conducted in a 3 l jar fermenter equipped with a Labo-controller (MDL-80, Marubishi, Tokyo Japan) with a 1.2 l working volume. The culture broth was centrifuged at 9,447 g and the supernatant was stored in a 4°C refrigerator. The activity of the cellulase was analyzed before use in the enzymatic hydrolysis of PSOM.
The inoculums of S. cerevisiae TJ14 was carried out in 50 g/l yeast/peptone/dextrose (YPD) medium containing less than 0.04% of adenine (Sigma-Aldrich Co. Ltd., St Louis, MO, USA). The YPD medium was composed of 20 g/l of bacteriological peptone, 10 g/l of yeast extract and 20 g/l of glucose. This seed culture was incubated for 24-30 h and by this time the cell density was about 2.2 to 2.8 g dry cell weight (DCW)/l. The fermentation was carried out by adding 10% (v/v) inoculum. The ethanol production medium was comprised (per liter) of 4 g KH2PO4, 2.5 g (NH4)2SO4, 0.6 g MgSO4·7H2O, 2.35 g K2C4H4O6·4H2O, 1.0 g CaCl2·2H2O, 5 g yeast extract and 10 g of polypeptone. Glucose was used as a carbon source during fermentation. In the case of ethanol production from PS, the medium was comprised (per liter) of PS, 5 g yeast extract, 10 g of polypeptone and 4 g KH2PO4 in 0.2 M maleic buffer. The quantity of PS used was varied for each experiment.
Optimization of saccharification
PSOM was hydrolyzed in 500 ml Erlenmeyer flasks in a reciprocal shaker at an agitation rate of 110 rpm for 120 h at 42°C in 0.8 M maleate buffer with initial pH 5.2 . The PSOM concentrations were varied 10, 30, 50, 70, 90, 110 g/l in maleate buffer. For the saccharification reaction, the Acremozyme cellulase (Meiji Seika Kaisha) used had an activity of 5, 10, 20, 40, 60, 80, 100 filter paper units (FPU)/g PSOM. Samples were taken every 12 h and centrifuged at 9,447 g for 5 min. The reaction was stopped by boiling the samples for 5 min and then measuring the RS content of the supernatant. Data were analyzed by Design Expert (v. 7.1.6, Stat-Ease, Minneapolis, MN, USA).
using a PSOM content of 24.5%.
Separate hydrolysis fermentation and simultaneous saccharification fermentation
SHF involves enzymatic hydrolysis and fermentation, and these were carried out in 500 ml Erlenmeyer flasks with a working volume of 100 ml. The PSOM was hydrolysed by cellulase produced from PSOM as carbon source until a maximum RS concentration was achieved. A total of 5 g/l of yeast extract, 10 g/l polypeptone and 4 g/l KH2PO4 were added to the hydrolysate and this mixture was used as the fermentation medium. The medium was also sterilized to deactivate the cellulase prior to fermentation. After the sterilized medium had been cooled to 42°C, it was inoculated with 10% (v/v) of the yeast preculture and incubated with agitation at 50-80 strokes per min (spm) in a reciprocal shaker (Bioshaker TA-25R, Takasaki Scientific Instruments, Saitama, Japan) and 42°C.
For improving ethanol concentration, PSOM concentration and cellulase activity were optimized using the following conditions: initial PSOM concentrations were 50, 80 and 110 g/l and cellulase activities were 15, 25 and 35 FPU/g PSOM. After medium sterilization, the cellulase and 10% inoculum were added to 500 ml Erlenmeyer flasks with final working volumes of 100 ml. When 170 g/l of PSOM and 35 FPU/g PSOM were used, the culture could not be readily mixed. To avoid the mixing problem, the PSOM was added at 0 and 8 h of culture time as follows: 8.5 g of PSOM (PS 34.7 g containing 22.5 ml of water), 14 ml of cellulase solution, 10 ml of inoculum, and 21 ml of buffer (total working volume of 67.5 ml), and at the culture time of 8 h, another 8.5 g PSOM (PS 34.7 g containing 22.5 ml of water) and 10 ml of cellulase solution were added. The final working volume was 100 ml. The PSOM concentration was 126 g/l at 0-8 h of culture time, and 170 g/l after 8 h of culture time.
To improve ethanol production in SSF, the amount of PSOM was increased with 15 FPU/g PSOM of cellulase. Due to mixing problems, the initial concentration was 80 g PSOM/l, and 11 g PSOM (44.9 g PS) and PS cellulase 15 FPU/g PSOM were added on one, two or three occasions at culture times of 8 h, 16 h, and 20 h, respectively. The final PSOM concentration was therefore 127, 151 and 165 g PSOM/l in each case. The SSF was conducted at 42°C until a maximum ethanol concentration was reached with agitation at 50-80 spm in a reciprocal shaker (Bioshaker TA-25R, Takasaki Scientific Instruments).
To improve ethanol yield, the inoculum was increased from 10% to 20% when the following conditions were used: 100 g/l of initial PSOM with 15 FPU/g PSOM, then 11 g PSOM added at culture times of 8 and 16 h. All PS used in the above experiments was sterilized to avoid contamination in the fermentation, and fermentation was stopped when the ethanol concentration reached a maximum. After SSF, the ethanol solution was separated from insoluble material of SSF culture broth. The supernatant was refrigerated at 4°C for measurement of RS, glucose, ethanol concentrations and remaining cellulase activity.
Scale up of SSF was carried out in 2 l Erlenmeyer flask with a working volume of 1.2 l. The initial composition of SSF was 100 PSOM g/l and 15 FPU/g PSOM, and the SSF was started with 20% inoculum in 600 ml. An additional 66 g of PSOM and 15 FPU/g PSOM of cellulase were added twice at culture times of 8 h and 16 h, and then final working volume adjusted to 1.2 l.
where C psom denote initial PSOM concentrations (g/l). Constants 1.11 and 0.51 denote coefficients from hydrolysis of glucan and from hexose to ethanol, respectively.
Cellulase activity was measured using the standard International Union of Pure and Applied Chemistry (IUPAC) procedure with Whatman no. 1 filter paper, and the activity was expressed in FPU. The FPU unit is based on the International Unit (IU) in which the absolute amount of glucose at a critical dilution is 2 mg for 0.5 ml critical enzyme concentration in 60 min .
The monosaccharide content was analyzed by high-performance liquid chromatography (HPLC; PU-980; JASCO Co. Ltd., Tokyo, Japan). Detection was carried out using a refractive index detector (RI-930, JASCO) and an amine-modified silica column (Shodex Asahipack NH2P-50 4E, 4.6 diameter, 250 mm, Shimadzu GLC Ltd., Tokyo, Japan) in combination with a precolumn. The mobile phase was 75% acetonitrile, and the flow rate was 1 ml/min. The total sugar content of PS was determined according to the standard National Renewable Energy Laboratory (NREL) method . PS was dried at 80°C and treated with 72% H2SO4 for 1 h at 30°C, then diluted with 4% H2SO4 and autoclaved for 1 h at 121°C. Glucose and mannose concentrations were analyzed with Megazyme kits (Biocon (Japan) Ltd., Nagoya, Japan) while the RS content of the medium was determined by the dinitrosalicylic acid method.
Ethanol concentration was measured using gas chromatography (GC) (Shimadzu-2014, Shimadzu Co. Ltd., Tokyo, Japan) using a packed column (Gaskuropack 54 60/80, GC-2014 Glass ID. 3.2 diameter × 2.1 m, GL Science Co. Ltd., Tokyo, Japan), with the following operational conditions: temperature of column and detector were 110°C and 250°C, respectively; nitrogen gas flow rate was 60 ml/min; injected sample volume was 2 μl.
Ethanol production from monosaccharide
Enzymatic hydrolysis of untreated PS using cellulase from PS origin
Comparison of ethanol production between SHF and SSF
In SSF, under conditions of 50 g/l PSOM with 15 FPU/g PSOM cellulase and 10% inoculum, the glucose and RS concentrations increased up to 4 h (Figure 4A). During the subsequent time period, the DCW increased to 0.6 g/l at 12 h and reached 12 g/l at 44 h (Figure 4B). The glucose concentration was found to be almost 0 g/l (Figure 4A), indicating that saccharification was the limiting step in ethanol production. The ethanol concentration reached 11.4 g/l at 44 h (Figure 4C). The maximum Ye/hex and Ye/psom were 57.4% and 21.4%, respectively.
The cellulase activity was investigated at SHF and SSF. In SHF, the glucose or RS concentration was higher than 8 g/l and 14 g/l at 12 h. High RS or glucose concentration might cause deactivation of cellulase [23, 24] (Figure 4D) because the hydrolysate rate decreased after that. However, during SSF, the enzyme activity remained at around 60% of initial activity (Figure 4D). However, the activity dropped below 10% of the initial activity before 4 h (Figure 4D). Initially, the glucose concentration was below 5 g/l and therefore did not deactivate cellulase, but insoluble materials contained in PS, for example clay and cellulose, adsorbed the cellulase. Since cellulase activity was assayed only in the supernatant, the cellulase adsorbed on the surface of cellulose and clay was excluded from the cellulase assay. Therefore, in the first 4 h, the measured cellulase activity was very low. However, at subsequent timepoints, with the progress of the hydrolysis of PSOM the cellulase detached from the surface of PSOM and insoluble materials and released to supernatant. As a result, the cellulase activity recovered.
These results show that SSF was preferable for ethanol production from PS. A method of semi-SSF that consisted of prehydrolysis and SSF was found to be unsuitable for this process, because of the long saccharification time and remaining high glucose concentration during reaction .
Improved ethanol production in SSF
In order to maximize ethanol concentration from PS, the PSOM amount (50-110 g/l) and cellulase activity (15-35 FPU/g PSOM) were optimized. Surface response (Expert design v. 7.1.6) showed ethanol production trends (Additional file 1) following the equation below:
To solve this problem, the amount of inoculum used was increased to 20%, with an initial PSOM concentration of 100 g/l, and two additions of 11.0 g PSOM (total PSOM concentration: 161 g/l). The ethanol concentration produced under these conditions increased from 35.7 to 40.5 g/l (Figure 6C) and Ye/hex improved to 66.3%. This process did not improve the ethanol production significantly. This was also confirmed in the 2 l Erlenmeyer flask with a working volume of 1.2 l, and the ethanol concentration reached 38.8 g/l with Ye/hex of 63.4% at a culture time of 72 h (data not shown).
In order to increase ethanol concentration, the PSOM concentration must be increased. To increase ethanol concentration to 40 g/l, two strategies were devised: increasing cellulase activity to solve glucose limitation, and increasing the fermentation inoculum to improve ethanol production. The cellulase activity was increased to 35 FPU/g PSOM to increase saccharification yield by around 5%. The ethanol concentration increased from 37 g/l to 40 g/l and the Ye/psom also increased from 21 to 24% (g ethanol/g PSOM). When 20% of the inoculum was used, the ethanol concentration, Ye/psom, and Ye/hex increased to 40.5 g/l, 24.2%, and 66.3%, respectively. This result was similar to that of bioconversion of Kraft paper mill sludge to ethanol using SSF . Ideal ethanol production from cellulose was observed for SF, since SF consists entirely of cellulose. Ye/cellulose using 50 g SF/l was 20.3% (data not shown), which is the same yield as that obtained using 50 g PSOM cellulose/l in SSF. Therefore, SSF of PS can be considered to be nearly the same as the ideal process using SF as carbon source.
Ys estimated 64% based on experimental data; 192 g PSOM used
Estimated sugar amount (g)
Theoretical glucose needed
38.8 g/l/0.51 × 1.2 l = 91.3
RS at the end fermentation
11 g/l × 1.2 l = 14.4
Glucose for yeast maintenance
ma (g/g cell/h) × 7.1 g/l × 72 h = 17.5
Total RS in hydrolysate
Estimated Ys (%)
123/192 × 100 = 64.0
The ethanol yield (Ye/psom) obtained when 50 to 150 g PSOM/l was used was 21% to 23% (g ethanol/g PSOM) in the SSF, which is two times higher than that obtained using SHF. Cellulase activity remained at around 60% throughout SSF. Within the PSOM concentrations less than 160 g PSOM/l, the ethanol yield remained at 23% with the ethanol concentration of 40 g/l. Ethanol production of 40 g/l was achieved using 161 g/l of PSOM with 15 FPU/g PSOM and 20% inoculum, after 80 h using the optimized SSF process. This was confirmed in the 2 l scale experiment and indicates that there is great potential to use PS as a raw material for ethanol production.
This study was supported by the Comprehensive Support Programs for Creation of Regional Innovation in Japan Science and Technology Agency (JST).
- Prasetyo J, Kato T, Park EY: Efficient cellulase-catalyzed saccharification of untreated paper sludge targeting for biorefinery. Biomass Bioenerg. 2010, 34: 1906-1913. 10.1016/j.biombioe.2010.07.021.View ArticleGoogle Scholar
- Claassen PAM, van Lier JB, Contreras AML, van Niel EWJ, Sijtsma L, Stams AJM, de Vries SS, Weusthuis RA: Utilisation of biomass for the supply of energy carriers. Appl Microbiol Biotechnol. 1999, 6: 741-755.View ArticleGoogle Scholar
- Solomon BD, Barnes JR, Halvorsen KE: Grain and cellulosic ethanol: history, economics, and energy policy. Biomass Bioenerg. 2007, 6: 416-425.View ArticleGoogle Scholar
- Yamashita Y, Sasaki C, Nakamura Y: Development of efficient system for ethanol production from paper sludge pretreated by ball milling and phosphoric acid. Carbohyd Polym. 2010, 79: 250-254. 10.1016/j.carbpol.2009.07.054.View ArticleGoogle Scholar
- Larsson S, Palmqvist E, Hahn-Hagerdal B, Tengborg C, Zacchi G, Nilvebrant NO: The generation of fermentation inhibitors during dilute acid hydrolysis of softwood. Enzyme Microb Technol. 1999, 24: 151-159. 10.1016/S0141-0229(98)00101-X.View ArticleGoogle Scholar
- Ranatunga TD, Jervis J, Helm RF, McMillan JD, Wooley RJ: The effect of overliming on the toxicity of dilute acid pretreated lignocellulosics: the role of inorganics, uronic acids and ether-soluble organics. Enzyme Microb Technol. 2000, 27: 240-247. 10.1016/S0141-0229(00)00216-7.View ArticleGoogle Scholar
- Shen J, Agblevor FA: Ethanol production of semi-simultaneous saccharification and fermentation from mixture of cotton gin waste and recycled paper sludge. Bioproc Biosyst Eng. 2010, 34: 33-43.View ArticleGoogle Scholar
- Matsushika A, Inoue H, Kodaki T, Sawayama S: Ethanol production from xylose in engineered S. cerevisiae strain: current state and perspectives. Appl Microbiol Biotechnol. 2009, 84: 37-53. 10.1007/s00253-009-2101-x.View ArticleGoogle Scholar
- Erdei B, Barta Z, Sipos B, Reczey K, Galbe M, Zacchi G: Ethanol production from mixtures of wheat straw and wheat meal. Biotechnol Biofuel. 2010, 3: 16-10.1186/1754-6834-3-16.View ArticleGoogle Scholar
- Fan Z, South C, Lyford K, Munsie J, van Walsum P, Lynd LR: Conversion of paper sludge to ethanol in semi continuous solid fed reactor. Bioproc Biosyst Eng. 2003, 26: 93-101. 10.1007/s00449-003-0337-x.View ArticleGoogle Scholar
- Moukamnerd C, Kino-oka M, Sugiyama M, Kaneko Y, Boonchird C, Harashima S, Noda H, Ninomiya K, Shioya S, Katakura Y: Ethanol production from biomass by repetitive solid-state fed-batch fermentation with continuous recovery of ethanol. Appl Microbiol Biotechnol. 2010, 88: 87-94. 10.1007/s00253-010-2716-y.View ArticleGoogle Scholar
- Prasetyo J, Zhu J, Kato T, Park EY: Efficient production of cellulase in the culture of A. cellulolyticus using untreated waste paper sludge. Biotechnol Progr. 2011, 1: 104-110.View ArticleGoogle Scholar
- Ando T, Sakamoto T, Sugiyama O, Hiyoshi K, Matsue N, Henmi T: Adsorption mechanism of Pb on paper sludge ash treated by NaoH hydrothermal reaction. Clay Sci. 2004, 12: 243-248.Google Scholar
- Ikeda Y, Hayashi H, Okuda N, Park EY: Efficient cellulase production by the filamentous fungus A. cellulolyticus. Biotechnol Progr. 2007, 23: 333-338. 10.1021/bp060201s.View ArticleGoogle Scholar
- Yamanobe T, Mitsuishi Y, Takasaki Y: Isolation of cellulolytic enzyme producing microorganism, culture conditions and some properties of the enzymes. Agric Biol Chem. 1987, 51: 65-74. 10.1271/bbb1961.51.65.View ArticleGoogle Scholar
- Kansarn S: A novel concept for the enzymatic degradation mechanism of native cellulose by A. cellulolyticus. [http://hdl.handle.net/10297/1453]
- Sugiyama M, Benjaphokee S, Auesukaree C, Asvarak T, Boonchird C, Harashima H: Yeast carbon neutral biotechnology,-high-temperature and acid tolerant strain for high-level bioethanol production. Proceedings of the Thailand-Japan Joint Symposium on Bioproduction by efficient utilization of Thai resources in the 20th Annual Meeting of The Thai Society for Biotechnology: Biotechnology for Health Care, 2008. 2008, Maha Sarakham University, Maha Sarakham, Thailand, 14-17.Google Scholar
- Brachmann CB, Davies A, Cost GJ, Caputo E, Li J, Hieter P, Boeke JD: Designer deletion strains derived from S. cerevisiae S288C: a useful set of strains and plasmids for PCR-mediated gene disruption and other applications. Yeast. 1998, 14: 115-132. 10.1002/(SICI)1097-0061(19980130)14:2<115::AID-YEA204>3.0.CO;2-2.View ArticleGoogle Scholar
- Zhang j, Shao X, Townsend OV, Lynd LR: Simultaneous saccharification and co-fermentation of paper sludge to ethanol by Saccharomyces cerevisiae RWB222-part I: kinetic modelling and parameters. Biotechnol Bioeng. 2009, 5: 920-931.View ArticleGoogle Scholar
- Ghose TK: Measurement of cellulase activities. International Union of Pure and Applied Chemistry. Pure Appl Chem. 1987, 59: 257-268. 10.1351/pac198759020257.Google Scholar
- Sluiter A, Hames B, Ruiz R, Scarlata C, Sluiter J, Templeton D: Determination of Structural Carbohydrates and Lignin in Biomass. 2004, Golden, CO, USA: National Renewable Energy LaboratoryGoogle Scholar
- Shuler ML, Kargi F: Bioprocess Engineering: Basic Concepts. 1992, Englewood Cliffs, NJ, USA: Prentice Hall PTS, 207-208.Google Scholar
- Zhang J, Heiss C, Thorne PG, Bal C, Azadi P, Lynda LR: Formation of ethyl β-xylopyranoside during simultaneous saccharification and co-fermentation of paper sludge. Enz Microb Technol. 2009, 44: 192-202.Google Scholar
- Kang L, Wang W, Lee YY: Bioconversion of kraft paper mill sludges to ethanol by SSF and SSCF. Appl Bichem Biotechnol. 2010, 161: 53-66. 10.1007/s12010-009-8893-4.View ArticleGoogle Scholar
- Rehnlund B: Blending of ethanol in gasoline for spark ignition engines. [http://www.eri.ucr.edu/ISAFXVCD/ISAFXVAB/BEGSIE.pdf]
- Egeback KE, Henke M, Rehnlund B, Wallin M, Westerholm R: Blending of ethanol in gasoline for spark ignition engines: Problem inventory and evaporative measurement. AVL-MTC. 2005, [http://www.growthenergy.org/images/reports/avl_ethanol_sparkignition.pdf] , Report number MTC 5407, ISSN: 1103-0240, ISRN: ASB-MTC-R-05/2-SEGoogle Scholar
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