Production of Fumaric Acid by Rhizopus oryzae in Simultaneous Saccharification and Fermentation using Xylo-Oligosaccharides Manufacturing Waste Residue
Xin Li,a,b,c Ximei Gu,c Chenhuan Lai,a,c Jia Ouyang,a,b,c and Qiang Yong a,b,c,*
Production of fumaric acid from xylo-oligosaccharides manufacturing waste residue (XOR) by Rhizopus oryzae CICC 40351 was investigated in a simultaneous saccharification and fermentation (SSF) process. The fermentation conditions for SSF were optimized by an orthogonal design method to maximize the fumaric acid concentration. The highest fumaric acid concentration (12.54 g/L) was reached with a substrate loading of 5% (w/v) XOR in the SSF process at 38 °C. The fumaric acid concentration of the SSF process was 1.8 times greater than that of the separate hydrolysis and fermentation (SHF) process under the same conditions. In addition, the SSF process yielded 0.34 g/g of glucose, whereas the SHF process yielded only 0.20 g/g of glucose. The results indicated that the SSF process notably improved the production of fumaric acid from lignocellulose by R. oryzae.
Keywords: Rhizopus oryzae; Fumaric acid; Simultaneous saccharification and fermentation; Lignocellulose
Contact information: a: Jiangsu Co-Innovation Center of Efficient Processing and Utilization of Forest Resources, Nanjing Forestry University, Nanjing 210037, Jiangsu Province, China; b: Key Laboratory of Forest Genetics & Biotechnology of the Ministry of Education, Nanjing Forestry University, Nanjing 210037, Jiangsu Province, China; c: College of Chemical Engineering, Nanjing Forestry University, Nanjing 210037, Jiangsu Province, China; *Corresponding author: email@example.com
Fumaric acid is a four-carbon unsaturated dicarboxylic acid. It serves as an important organic material and bulk chemical. Fumaric acid has been used as a food acidulant, beverage ingredient, and antibacterial agent (Xu et al. 2012). Fumaric acid is also used to produce polymers and resins due to a carbon-carbon double bond and two carboxylic acid groups in its structure (Roa Engel et al. 2008; Xu et al. 2012). In the 1940s, Pfizer developed an industrial fermentative process by Rhizopus arrhizus for production of fumaric acid with an annual production of 4000 tons (Goldberg et al. 2006). Because of higher raw material cost, lower fumaric acid concentration, lower yield, and lower productivity, the fermentative production of fumaric acid did not compete economically with a chemical process (Xu et al. 2012). Consequently, the fermentative production of fumaric acid was stopped in the 1970s and replaced by a more economical chemical process from petrochemical feedstocks (Goldberg et al. 2006; Roa Engel et al. 2008; Xu et al.2012). Fumaric acid is currently synthesized by isomerization of maleic acid with an annual production of 90,000 tons (Roa Engel et al. 2008); however, the chemical process causes environmental problems, including toxic airborne pollution and water pollution. With increasing concern over sustainability and consumer preference for natural products, the discovery of an economical biotechnological route for producing fumaric acid has gained a renewed attention from researchers.
The Rhizopus genus, grown on simple nutrients required for fermentation, contains strains used for fumaric acid production, especially Rhizopus oryzae (Huang et al. 2010). Roa Engel et al.(2008) reported that fermentative production of fumaric acid was mainly from glucose and starch-based materials. However, glucose is an expensive carbon source, and starch-based materials as feedstock are inevitably facing the challenge of the increased food security (Valentine et al.2012). Therefore, the cheaper, abundant, and non-edible feedstock is crucial for fermentative production of fumaric acid by Rhizopus oryzae. Some studies have focused on seeking a suitable feedstock, such as wheat bran (Wang et al. 2015), pulp and paper solid waste (Das et al. 2016), apple industry waste biomass (Das et al. 2015a), brewery wastewater (Das et al. 2015b), corn straw (Xu et al. 2010), and dairy manure hydrolysate (Liao et al. 2008). Lignocellulosic materials (especially wood and agricultural residues) are promising potential alternatives for biorefinery characterized by renewable, cheap, abundant, and non-edible biomass. Rhizopus oryzae is a suitable strain for the production of fumaric acid using lignocellulose-based carbohydrate as a carbon source. A two-stage corn straw utilization strategy was reported to convert concentrated glucose into 27.79 g/L fumaric acid, with a glucose yield of 0.35 g/g (Xu et al. 2010). Rhizopus oryzae (ATCC 20344) was added to dairy manure hydrolysate (lignocellulosic material) and pure glucose to produce 31 g/L of fumaric acid, with a yield of 31% (Liao et al. 2008). These experiments required the enzymatic hydrolysis of pretreated lignocellulosic materials before fermentation, which is described as a separate hydrolysis and fermentation (SHF) process. In recent literature, fermentative production of fumaric acid has been carried out mainly through submerged fermentation (Liao et al. 2008; Xu et al. 2010; Das et al. 2015a; Wang et al. 2015; Das et al. 2016), solid state fermentation (Das et al. 2015a; Das et al. 2016), or immobilized submerged fermentation (Das et al. 2015b). Different from recent studies, we developed a simultaneous saccharification and fermentation (SSF) process for production of fumaric acid from lignocellulose by R. oryzae. A SSF process was carried out using enzymatic hydrolysis of lignocellulose and the fermentation of releasing sugars in the same vessel. In comparison with SSF, SHF may pose several problems, such as end-product inhibition of enzymatic hydrolysis, lower hydrolysis rate, lower yield, and lower product concentration.
The present study investigated the production of fumaric acid using SSF of xylo-oligosaccharides manufacturing waste residue (XOR) with R. oryzae (CICC 40351). The XOR was a cellulose-rich solid residue resulted from the alkali-pretreatment of corncobs. Optimization of key factors using SSF was carried out according to an orthogonal design. A commercial cellulase with supplemental β-glucosidase was used for the enzymatic hydrolysis of cellulose.
R. oryzae CICC 40351 was purchased from the China Center of Industrial Culture Collection (CICC; Beijing, China).
Xylo-oligosaccharides manufacturing waste residue
XOR was a gift from the Jiangsu Kangwei Biologic Co., Ltd. (Dongtai, Jiangsu Province, China). The XOR was a cellulose-rich solid residue from the alkali-pretreatment of corncobs. The corncobs were pretreated in 7% (w/v) sodium hydroxide solution for 1 h at 85 to 90 °C. After solid/liquid separation by filtration, the liquid fraction containing hemicellulose was used for the production of xylo-oligosaccharides. The solid fraction was soaked in water at a solid-liquid ratio of 1:10 (w/v) and then neutralized by 72% (w/w) sulfuric acid to a pH of 4.8 to 5.0. The mixture was filtered to remove the liquid fraction to obtain the solid fraction (named XOR). And the XOR was stored in plastic bags at 4 °C.
Cellulase and β-glucosidase were purchased from Sigma Aldrich (Novozymes, Bagsvaerd, Denmark) and used without further purification.
The composition of the slant medium was as follows: 10.0 g/L glucose, 3.0 g/L yeast extract, 3.0 g/L malt extract, 5.0 g/L peptone, and 20.0 g/L agar. The inoculated slant was cultured in an incubator at 30 °C for one week and then stored at 4 °C until further use.
The seed medium was composed of the following: 40 g/L glucose, 4.4 g/L (NH4)2SO4, 0.5 g/L MgSO4∙7H2O, 0.6 g/L KH2PO4, 0.0176 g/L ZnSO4∙7H2O, and 0.000498 g/L FeSO4∙7H2O.
The spores were washed from the slant with sterile water, and the spore density was adjusted to107 spores per milliliter.
The SSF medium consisted of the following: 5% (w/v) XOR, 0.71 g/L (NH4)2SO4, 0.5 g/L MgSO4∙7H2O, 0.6 g/L KH2PO4, 0.01 g/L ZnSO4∙7H2O, 0.0004 g/L FeSO4∙7H2O, and 30 g/L CaCO3 in 0.05 mol/L sodium acetate-acetic acid (NaOAc-AcH) buffer (pH of 4.8).
The SHF medium consisted of the following: enzymatic hydrolysate at 5% (w/v) XOR, 0.71 g/L (NH4)2SO4, 0.5 g/L MgSO4∙7H2O, 0.6 g/L KH2PO4, 0.01 g/L ZnSO4∙7H2O, 0.0004 g/L FeSO4∙7H2O, and 30 g/L CaCO3.
All chemicals used in the present work were analytical grade without further purification.
Enzymatic hydrolysis of 5% (w/v) XOR was conducted in an incubator at 50 °C and 150 rpm. The dosages of cellulase and β-glucosidase were 25 FPIU/(g cellulose) and 20 IU/(g cellulose), respectively. The glucose yield was calculated as follows:
Glucose yield (%) = Glucose (g) × 0.9 ×100 / initial [cellulose] in substrate (g) (1)
The seed suspension was transferred to the medium and cultured in an incubator (New Brunswick Scientific, INNOVA 40R, USA) for 24 h at 35 °C and 200 rpm.
Simultaneous saccharification and fermentation (SSF)
The SSF was conducted using free enzymes (cellulase and β-glucosidase) at 38 °C and 220 rpm in fermentation medium (50 mL) with a 10% (v/v) inoculum.
Separated hydrolysis and fermentation (SHF)
Enzymatic hydrolysis of 5% (w/v) XOR was conducted using a cellulase cocktail at 50 °C and 150 rpm. The supernatant resulting from enzymatic hydrolysate was obtained by centrifugation at 5000 rpm for 10 min. The supernatant and other fermentation medium components comprised the SHF medium. Fermentation of the SHF medium was carried out in an incubator at 38 °C and 220 rpm.
The fumaric acid, ethanol, and glucose concentrations were determined by high performance liquid chromatography (HPLC, Agilent Technologies, 1260 Infinity, USA) equipped with a Bio-Rad Aminex HPX-87H column and a refractive index detector. The mobile phase was 5 mM H2SO4, and the flow rate was maintained at 0.6 mL/min.
Because of the low solubility of fumaric acid at room temperature (Lange and Sinks 1930), the final culture broth was treated with 25% (w/w) NaOH solution to convert fumaric acid into soluble sodium fumarate. The excess NaOH was neutralized with 36% (w/w) H2SO4 solution before the samples were tested.
The analysis of chemical composition of XOR was carried out according to the National Renewable Energy Laboratory standard method for the determination of structural carbohydrates and lignin in biomass (Sluiter et al. 2008). Filter paper and β-glucosidase activities were determined according to the International Union of Pure and Applied Chemistry procedures (Ghose 1987). One FPIU was deﬁned as the amount of enzyme needed to release 1 μmol of glucose equivalent from Whatman No.1 ﬁlter paper per min. One unit of β-glucosidase was deﬁned as the amount of enzyme needed to convert 1μmol of cellobiose to 2 μmol of glucose per min.
Mycelial biomass was washed with deionized water after neutralization of residual CaCO3 in fermentation medium by 6 M hydrochloric acid. Then, the biomass was dried at 65 °C until a constant weight was obtained.
All the data are presented as the mean of two experiments. All the experiments were carried out in 250-mL flasks containing 50 mL of medium.
RESULTS AND DISCUSSION
Xylo-Oligosaccharides Manufacturing Waste Residue (XOR) and Enzymatic Hydrolysis
After the corncob was treated with sodium hydroxide, the compositional comparison of raw material and XOR was obtained (Table 1). The corncob contained (% dry wt.) 36.01% cellulose, 36.84% hemicellulose, 17.43% lignin (including acid-soluble lignin and acid-insoluble lignin), and 3.43% ash. After the alkali pretreatment, XOR contained 66.95% cellulose, 21.87% hemicellulose, 5.92% lignin (including acid-soluble lignin and acid-insoluble lignin), and 1.20% ash. The percentage of glucan after the pretreatment increased from 36.01% to 66.95% because of the solubilization of xylan. The alkali pretreatment effectively decreased the hemicellulose and lignin fractions of the lignocellulosic materials (Kim and Holtzapple 2006; Qin et al. 2010).
The 48-h enzymatic hydrolysis of 5% (w/v) XOR released 34.97 g/L of glucose (Fig. 1). The glucose yield after the hydrolysis of XOR was greater than 94%. The alkali pretreatment removed most of the hemicellulose and a portion of lignin. The removal of hemicellulose and lignin was beneficial for improving the glucose yield due to the strong structural modification of lignocellulosic material caused by pretreatment (Mussatto et al. 2008).
Table 1. Comparison of Corncob and Xylo-Oligosaccharides Manufacturing Waste Residue (XOR) (% dry wt.)
Values represent the mean ± standard deviation
Fig. 1. Time-course of glucose production during enzymatic hydrolysis at 50 °C
Selection of Temperatures for SSF Processing
The processing temperature is a key factor for both cellulase hydrolysis and fermentation of SSF (Narra et al. 2015). Generally, the optimum temperature of cellulase hydrolysis ranged from 48 °C to 50 °C (Xu et al. 2009; Rodríguez-López et al. 2012), and the optimum temperature of fermentation for R. oryzae ranged from 30 °C to 35 °C (Liao et al. 2008; Kang et al. 2010; Ding et al. 2011; Deng et al. 2012). No substantial growth of R. oryzae was observed over 40 °C (Gao et al. 2011). Therefore, it was crucial for SSF with R. oryzae to select a proper temperature closer to the optimal temperature of cellulase hydrolysis.
Figure 2 and Table 2 show the effect of R. oryzae on glucose utilization at different temperatures. As shown in Fig. 2, R. oryzae consumed glucose at 35 and 38 °C after 24 h of fermentation; however, 10 g/L glucose was observed in the broth after 60 h of fermentation when thetemperature was increased to 41 °C. Increasing the temperature beyond a certain point decreased the consumption of glucose and limited the fermentation capacity of R. oryzae. Table 2 shows a decrease in fumaric acid concentration with increasing temperature within the range of 35 to 41 °C. R. oryzae produced 7.56 g/L of fumaric acid, with a yield of 0.19 g/g glucose and a productivity of 0.13 g/(L·h) at 38 °C, which was similar to that at 35 °C. The biomass of R. oryzae was maintained at a relatively constant level (Zhou et al. 2011).
Table 2. Product Concentrations after 60 h of Fermentation
*g fumaric acid/g glucose
ND: not detected
Values represent the mean ± standard deviation
Fig. 2. Glucose consumption by R. oryzae over time
Enzymatic hydrolysis of XOR at 38 °C was investigated at the same cellulase concentration. A comparison of enzymatic hydrolysis at 5% (w/v) XOR at 38 and 50 °C is shown in Table 3. A slightly lower glucose concentration (32.23 g/L) at 38 °C was observed compared to 34.97 g/L at 50 °C. A more accumulated cellobiose was found at 38 °C because of the lower β-glucosidase activity at 38 °C. The glucose yield at 38 °C was 9.91% lower than that at 50 °C. Kaar and Holtzapple (2000) found that there was a minimal difference in the enzymatic hydrolysis of alkali-treated corn stover between 40 and 50 °C (Kaar and Holtzapple 2000). Cellulase hydrolysis showed a better glucose yield at a lower temperature. Therefore, 38 °C was used for SSF in the following experiments.
Table 3. Effect of Temperature on Enzymatic Hydrolysis Products
Values represent the mean ± standard deviation
Orthogonal Design for Optimizing Fermentation Conditions of SSF
Nitrogen limitation influences the growth of R. oryzae when cells secrete fumaric acid (Gao et al.2011). Calcium carbonate and inoculum have an effect on the growth of R. oryzae mycelia (Liao et al. 2007). The dosage of cellulase is related to the economic efficiency of the process (Wahono et al. 2014). Therefore, ammonium sulfate (A), calcium carbonate (B), dosage of cellulase (C) and inoculum (D) were taken into account for production of fumaric acid during the SSF process by R. oryzae. The orthogonal design of the SSF conditions and the analysis of results are shown in Tables 4 and 5, respectively.
Table 4. Factors and Levels of the Orthogonal Design L9 (34) for SSF
Table 5. Results of the Orthogonal Design
Order: D > A > B > C; Optimal scheme: D3A1B2C2
a: the sum of fumaric acid concentration for each factor at different levels
b: the means of fumaric acid concentration for each factor at different levels
c: the ranges of fumaric acid concentration for each factor at different levels
The effects of SSF conditions on the production of fumaric acid decreased in the order, D > A > B > C, based on the RangR values (Table 5). According to the fumaric acid concentration for each factor level, the maximum fumaric acid concentration (12.54 g/L) was obtained at 0.71 g/L ammonium sulfate, 30 g/L calcium carbonate, 25 FPIU cellulase/g cellulose, and 15% (v/v) inoculum.
Comparison of SSF and SHF
The process of SSF was applied for the production of fumaric acid with lignocellulose by R. oryzae. Fumaric acid was produced from 5% (w/v) XOR during the SSF process. The SSF was compared with SHF at a 5% (w/v) substrate loading rate. The substrate loading rate of 5% (w/v) was chosen to avoid the propensity for viscous conditions resulting from high substrate loading (Tomás-Pejó et al. 2008). In SHF, hydrolysate containing 33.67 g/L glucose was used as the sole carbon source, which resulted from the enzymatic hydrolysis of 5% (w/v) XOR.
Figure 3 shows the sugar consumption from SSF and SHF. The SHF process showed a 24-h lag phase at the beginning of fermentation, and the glucose concentration remained relatively constant during the first 24 h of fermentation. This indicated that the R. oryzae required 24 h of adaption to lignocellulosic hydrolysate during SHF. Fortunately, SSF reduced the lag phase and enhanced R. oryzae tolerance to lignocellulosic hydrolysate of XOR. Enzymatic hydrolysis of XOR for 24 h released greater than 30 g/L of glucose (Fig. 1), while SSF, at the same dosage of cellulose, released less than 20 g/L of glucose (Fig. 3). Consequently, R. oryzae consumed approximately 30% of the glucose released from the enzymatic hydrolysis of XOR during the first 24 h of SSF. Obviously, the strain easily adapted to the environmental conditions of the SSF process (Pietrzak and Kawa-Rygielska 2015).
After 24 h of fermentation, the R. oryzae in SHF consumed sugars faster than SSF. Glucose was exhausted at 60 h for both processes. Table 6 shows that fumaric acid reached 12.54 g/L after 60 h of SSF, while only 6.76 g/L was obtained by SHF. The SSF process increased 85.5% of the fumaric acid concentration and demonstrated a better yield of fumaric acid (0.34 g/g) overall. The SSF process notably increased the fumaric acid yield from 0.20 to 0.34 g/g using XOR as carbon source.
Several studies on the production of fumaric acid from lignocellulosic materials have been reported and are summarized in Table 7. Xu et al. (2010) reported a two-stage process for fumaric acid production from corn straw, with a fumaric acid yield of 0.35 g/g. R. oryzae initially grew in the xylose-rich hydrolysate from acid hydrolysis of corn straw, and then was transferred into the glucose-rich hydrolysate from enzymatic hydrolysis of the acid-pretreated corn straw. The whole process required over 182 h, including the processes of enzymatic hydrolysis and concentration (Xu et al. 2010).
The SSF process reported herein provided a one-pot process for fumaric acid production with lignocellulosic material and achieved a fumaric acid yield of 0.34 g/g. Liao et al. (2008) showed that R. oryzae ATCC 20344 yielded fumaric acid with a fumaric acid yield of 0.31 g/g from dairy manure hydrolysate with the addition of pure glucose. However, the hydrolysate only contained approximately 20% to 26% glucose from dairy manure, and 74% to 80% glucose was contributed from pure glucose (Liao et al. 2008). In this article, XOR was directly sourced as the sole carbon input for fumaric acid production. The fumaric acid concentration from the SSF process was greater than that from the SHF process under the same conditions.
During fermentative production of fumaric acid, ethanol is the primary by-product in the metabolic pathways of R. oryzae, and the formation of ethanol reduces the carbon flux to fumaric acid (Xu et al. 2012). As shown in Table 6, the ethanol concentrations in SSF and SHF were 2.64 g/L and 3.20 g/L, respectively. The difference in ethanol concentration was at a low level between SSF and SHF. The SSF process showed a slight effect on carbon flux toward ethanol formation. Therefore, the results show that SSF was a better process for the production of fumaric acid using lignocellulose as the raw material. However, the production of fumaric acid by SSF is still facing some problems, such as the low fumaric acid concentration obtained in the present work.
Increased solids loading led to higher potential product concentration, reducing equipment’s size, energy consumption, and the burden of the downstream processing (Romaní et al. 2012). From the economic point of view, higher fumaric acid concentration is beneficial for the large-scale production of fumaric acid. Further study would focus on fermentative production of fumaric acid by SSF at high solid loading to achieve higher fumaric acid concentration.
Table 6. Comparison of Fumaric Acid Yield and Productivity
*g fumaric acid/g glucose
SSF: Simultaneous saccharification and fermentation
SHF: Separate hydrolysis and fermentation
Table 7. Fumaric Acid Production from Lignocellulosic Materials by Rhizopus oryzae
SSF: Simultaneous saccharification and fermentation
SHF: Separate hydrolysis and fermentation
XOR: Xylo-oligosaccharides manufacturing waste residue
Fig. 3. A comparison of glucose consumption between SSF and SHF over time. SSF: Simultaneous saccharification and fermentation; SHF: Separate hydrolysis and fermentation.
- A SSF process was developed for production of fumaric acid from lignocellulose by R. oryzae.
- Optimization of SSF conditions was carried out by an orthogonal design. The processes of SSF and SHF were carried out for the production of fumaric acid from low-cost lignocellulose by R. oryzae. The SSF at 38 °C obtained the greatest fumaric acid concentration (12.54 g/L) from 5% (w/v) XOR compared with 6.76 g/L fumaric acid from the SHF process during the same conditions.
- The SSF process notably improved the production of fumaric acid from XOR by R. oryzae.
The authors are grateful for support from the Major Program of the Natural Science Foundation of Jiangsu Higher Education (14KJA220003), the Natural Science Foundation of Jiangsu Province (Grant No. BK20131426), the Key Research and Development Program of Jiangsu Province (BF2015007), and the Priority Academic Program Development of the Jiangsu Higher Education Institutions (PAPD).
Das, R. K., Brar, S. K., and Verma, M. (2015a). “A fermentative approach towards optimizing directed biosynthesis of fumaric acid by Rhizopus oryzae 1526 utilizing apple industry waste biomass,” Fungal Biology 119(12), 1279-1290. DOI: 10.1016/j.funbio.2015.10.001
Das, R. K., Brar, S. K., and Verma, M. (2015b). “Enhanced fumaric acid production from brewery wastewater by immobilization technique,” Journal of Chemical Technology and Biotechnology90(8), 1473-1479. DOI: 10.1002/jctb.4455
Das, R. K., Brar, S. K., and Verma, M. (2016). “Potential use of pulp and paper solid waste for the bio-production of fumaric acid through submerged and solid state fermentation,” Journal of Cleaner Production 112, 4435-4444. DOI: 10.1016/j.jclepro.2015.08.108
Deng, Y., Li, S., Xu, Q., Gao, M., and Huang, H. (2012). “Production of fumaric acid by simultaneous saccharification and fermentation of starchy materials with 2-deoxyglucose-resistant mutant strains of Rhizopus oryzae,” Bioresource Technology 107, 363-367. DOI: 10.1016/j.biortech.2011.11.117
Ding, Y., Li, S., Dou, C., Yu, Y., and Huang, H. (2011). “Production of fumaric acid by Rhizopus oryzae: Role of carbon–nitrogen ratio,” Applied Biochemistry and Biotechnology 164(8), 1461-1467. DOI: 10.1007/s12010-011-9226-y
Gao, C., Ma, C., and Xu, P. (2011). “Biotechnological routes based on lactic acid production from biomass,” Biotechnology Advances 29(6), 930-939. DOI: 10.1016/j.biotechadv.2011.07.022
Ghose, T. K. (1987). “Measurement of cellulase activities,” Pure and Applied Chemistry 59(2), 257-268. DOI: 10.1351/pac198759020257
Goldberg, I., Rokem, J. S., and Pines, O. (2006). “Organic acids: Old metabolites, new themes,” Journal of Chemical Technology and Biotechnology 81, 1601-1611. DOI: 10.1002/jctb.1590
Huang, L., Wei, P., Zang, R., Xu, Z., and Cen, P. (2010). “High-throughput screening of high-yield colonies of Rhizopus oryzae for enhanced production of fumaric acid,” Annals of Microbiology 60(2), 287-292. DOI: 10.1007/s13213-010-0039-y
Kaar, W. E., and Holtzapple, M. T. (2000). “Using lime pretreatment to facilitate the enzymic hydrolysis of corn stover,” Biomass and Bioenergy 18(3), 189-199. DOI: 10.1016/S0961-9534(99)00091-4
Kang, S. W., Lee, H., Kim, D., Lee, D., Kim, S., Chun, G. T., Lee, J., Kim, S. W., and Park, C. (2010). “Strain development and medium optimization for fumaric acid production,” Biotechnology and Bioprocess Engineering 15(5), 761-769. DOI: 10.1007/s12257-010-0081-4
Kim, S., and Holtzapple, M. T. (2006). “Deligniﬁcation kinetics of corn stover in lime pretreatment,” Bioresource Technology 97(5), 778-785. DOI: 10.1016/j.biortech.2005.04.002
Lange, N. A., and Sinks, M. H. (1930). “The solubility, specific gravity and index of refraction of aqueous solutions of fumaric, maleic and i-malic acids,” Journal of the American Chemical Society 52(7), 2602-2604. DOI: 10.1021/ja01370a003
Liao, W., Liu, Y., Frear, C., and Chen, S. (2007). “A new approach of pellet formation of a filamentous fungus – Rhizopus oryzae,” Bioresource Technology 98(18), 3415-3423. DOI: 10.1016/j.biortech.2006.10.028
Liao, W., Liu, Y., Frear, C., and Chen, S. L. (2008). “Co-production of fumaric acid and chitin from a nitrogen-rich lignocellulosic material – dairy manure – using a pelletized ﬁlamentous fungus Rhizopus oryzae ATCC 20344,” Bioresource Technology 99(13), 5859-5866. DOI: 10.1016/j.biortech.2007.10.006
Mussatto, S. I., Fernandes, M., Milagres, A. M. F., and Roberto, I. C. (2008). “Effect of hemicellulose and lignin on enzymatic hydrolysis of cellulose from brewer’s spent grain,” Enzyme and Microbial Technology 43(2), 124-129. DOI: 10.1016/j.enzmictec.2007.11.006
Narra, M., James, J. P., and Balasubramanian, V. (2015). “Simultaneous sacchariﬁcation and fermentation of deligniﬁed lignocellulosic biomass at high solid loadings by a newly isolated thermotolerant Kluyveromyces sp. for ethanol production,” Bioresource Technology 179, 331-338. DOI: 10.1016/j.biortech.2014.11.116
Pietrzak, W. and Kawa-Rygielska, J. (2015). “Simultaneous sacchariﬁcation and ethanol fermentation of waste wheat–rye bread at very high solids loading: Effect of enzymatic liquefaction conditions,” Fuel 147, 236-242. DOI: 10.1016/j.fuel.2015.01.057
Qin, W., Chen, Y., Zhao, H., Wang, R., and Xiao, D. (2010). “Optimization of pretreatment conditions for corn cob with alkali liquor,” Transactions of the Chinese Society of Agricultural Engineering 26(4), 248-253. DOI: 10.3969/j.issn.1002-6819.2010.4.042
Roa Engel, C. A., Straathof, A. J. J., Zijlmans, T. W., van Gulik, W. M., and van der Wielen, L. A. M. (2008). “Fumaric acid production by fermentation,” Applied Microbiolgy and Biotechnology78(3), 379-389. DOI: 10.1007/s00253-007-1341-x
Rodríguez-López, J., José Sánchez, A., María Gómez, D., Romaní, A., and Parajó, J. C. (2012). “Fermentative production of fumaric acid from Eucalyptus globulus wood hydrolyzates,” Journal of Chemical Technology and Biotechnology 87(7), 1036-1040. DOI: 10.1002/jctb.2729
Romaní, A., Garrote, G., and Parajó, J. C. (2012). “Bioethanol production from autohydrolyzed Eucalyptus globulus by simultaneous saccharification and fermentation operating at high solids loading,” Fuel 94, 305-312. DOI: 10.1016/j.fuel.2011.12.013
Sluiter, A., Hames, B., Ruiz, R., Scarlata, C., Sluiter, J., Templeton, D., and Crocker, D. (2008). Determination of Structural Carbohydrates and Lignin in Biomass (NREL/TP-510-42618), National Renewable Energy Laboratory, Golden, CO.
Tomás-Pejó, E., Oliva, J. M., Ballesteros, M., and Olsson, L. (2008). “Comparison of SHF and SSF processes from steam-exploded wheat straw for ethanol production by xylose-fermenting and robust glucose-fermenting Saccharomyces cerevisiae strains,” Biotechnology and Bioengineering100(6), 1122-1131. DOI: 10.1002/bit.21849
Valentine, J., Clifton-Brown, J., Hastings, A., Robson, P., Allison, G., and Smith, P. (2012). “Food vs. fuel: The use of land for lignocellulosic ‘next generation’ energy crops that minimize competition with primary food production,” GCB Bioenergy 4, 1-19. DOI: 10.1111/j.1757-1707.2011.01111.x
Wahono, S. K., Darsih, C., Rosyida, V. T., Maryana, R., and Pratiwi, D. (2014). “Optimization of cellulose enzyme in the simultaneous saccharification and fermentation of sugarcane bagasse on the second-generation bioethanol production technology,” Energy Procedia 47, 268-272. DOI: 10.1016/j.egypro.2014.01.224
Wang, G., Huang, D., Li, Y., Wen, J., and Jia, X. (2015). “A metabolic-based approach to improve xylose utilization for fumaric acid production from acid pretreated wheat bran by Rhizopus oryzae,” Bioreource Technology 180, 119-127. DOI: 10.1016/j.biortech.2014.12.091
Xu, J., Thomsen, M. H., and Thomsen, A. B. (2009). “Enzymatic hydrolysis and fermentability of corn stover pretreated by lactic acid and/or acetic acid,” Journal of Biotechnology 139(4), 300-305. DOI: 10.1016/j.jbiotec.2008.12.017
Xu, Q., Li, S., Fu, Y. Q., Tai, C., and Huang, H. (2010). “Two-stage utilization of corn straw by Rhizopus oryzae for fumaric acid production,” Bioresource Technology 101(15), 6262-6264. DOI: 10.1016/j.biortech.2010.02.086
Xu, Q., Li, S., Huang, H., and Wen, J. (2012). “Key technologies for the industrial production of fumaric acid by fermentation,” Biotechnology Advances 30, 1685-1696. DOI: 10.1016/j.biotechadv.2012.08.007
Zhou, Z., Du, G., Hua, Z., Zhou, J., and Chen, J. (2011). “Optimization of fumaric acid production by Rhizopus delemar based on the morphology formation,” Bioresource Technology 102(20), 9345-9349. DOI: 10.1016/j.biortech.2011.07.120
Article submitted: May 13, 2016; Peer review completed: July 11, 2016; Revised version received and accepted: August 16, 2016; Published: August 31, 2016.