Industrial cellulase performance in the simultaneous saccharification and co-fermentation (SSCF) of corn stover for high-titer ethanol production
© The Author(s) 2017
Received: 4 March 2017
Accepted: 25 March 2017
Published: 6 April 2017
Cellulase enzymes contribute to the largest portion of operation cost on production of cellulosic ethanol. The industrial cellulases available on the industrial enzyme market from different makers and sources vary significantly in hydrolysis and ethanol, and finally lead to the changes of enzyme cost. Therefore, the selection of the proper industrial cellulase enzymes for commercial-scale production of cellulosic ethanol is crucially important in terms of high performance and cost reduction.
In this study, three major cellulase enzyme products available on the Chinese industrial enzyme market were selected and evaluated as the biocatalysts for the biorefining process of lignocellulose biomass into high-titer ethanol. The cellulase enzymes included Cellic CTec 2.0 from Novozymes (Beijing), and LLC 4 from Vland (Qingdao), as well as # 7 from an industrial enzyme maker. The detailed assays on the filter paper activity, the cellobiase activity, and the total protein contents of the enzymes were conducted according to the standard protocols. When the cellulase enzymes were applied to the practical hydrolysis and ethanol-fermentation operation under the conditions of high solids loading and low range of cellulase dosage, the hydrolysis yield shows the significant difference, and the difference was narrowed in the final ethanol yield.
The commercially available cellulase enzymes showed different performances in the activities, the cellulose hydrolysis yield, and the ethanol fermentation yields based on the protein dosage per gram of cellulose of corn stover. In general, the industrial cellulase products give satisfactory performance and can be applied for the practical cellulosic ethanol production on commercial scale.
KeywordsIndustrial cellulase enzyme Activity Ethanol Hydrolysis Lignocellulose
Currently cellulosic ethanol is on the way to its large scale commercialization in USA, Europe, and China. Beta renewables first launched the first commercial cellulosic ethanol plant with the annual ethanol production of 40,000 metric tons from corn stover in Oct 2013, Italy (Ramesh 2013). DuPont biofuels solution started the plant for production of 89,600 metric tons of ethanol annually from corn stover and switchgrass. Abengoa Bioenergy produced 74,900 metric tons of ethanol annually from corn stover and other non-feed energy crops. Poet-DSM produced 59,700 metric tons of ethanol annually from corn stover (Chiaramonti et al. 2013). In China, Shandong Longlive Co. used corncob residue from xylitol industry and produced 50,000 metric tons of ethanol (Lei et al. 2014). However, due to the reasons of low petroleum price and relatively high cost, the factories are not operated in full scale and further modifications on the plants are still going on.
In the trend of commercialization of cellulosic ethanol, a proper cellulase enzyme with high hydrolysis performance and low cost is crucially important because cellulase enzyme contributes to the largest portion of the cost on lignocellulose biorefining process (Klein-Marcuschamer et al. 2012; Gang et al. 2016). In the past several decades, great efforts were made by the enzyme industry worldwide, and several high-performance cellulase enzymes had been developed and introduced into the market for practical use in cellulosic ethanol production. The latest cellulase enzyme products include the CTec series from Novozymes, such as the recent products of Cellic CTec 2, Cellic CTec 3, and HTec 3 (Chen et al. 2016); and the Accellerase series from the former Genencor (now part of DuPont), such as Accellerase 1500 (Marcos et al. 2013). On the Chinese industrial enzyme market, several homemade cellulase enzymes are available for use in cellulosic ethanol production (Zhang et al. 2015, 2016; Liu and Wang 2014).
In this study, we selected three major cellulase enzyme products available on the China industrial market including Cellic CTec 2.0 from Novozyme (Beijing), LLC 4 from Vland (Qingdao), and # 7 from an industrial enzyme maker as the saccharification biocatalyst of corn stover. The lignocellulose feedstock, corn stover, was pretreated by dry dilute acid pretreatment (DDAP) and biologically detoxified to remove the inhibitors, then hydrolyzed at the high solids loading (30%, w/w) of the pretreated and detoxified corn stover. The ethanol fermentation was performed under the simultaneous saccharification and co-fermentation (SSCF) by a xylose utilizing yeast strain to achieve the high-titer ethanol and yield. The results indicate that the industrial enzymes available as cellulase products in the market give the satisfactory performance in general and can be applied for the practical cellulosic ethanol production on commercial scale.
Corn stover feedstock
Corn stover (CS) was harvested from Bayan Nur League, Inner Mongolia Autonomous Region, China in fall 2015. The collected corn stover was milled coarsely and screened through a mesh with the circle diameter of 10 mm. Then the milled corn stover was water washed to remove the field dirts, stones and metal pieces, and air dried. The composition of corn stover was determined by the two-step acid hydrolysis method according to National Renewable Energy Laboratory (NREL) protocols (Sluiter et al. 2008, 2012). On dry weight base (w/w), corn stover contained 35.4% of cellulose, 24.6% of hemicellulose, 16.1% of lignin, and 3.5% of ash.
We selected three representative commercial cellulases from the Chinese industrial enzyme market, by the availability, the production capacity, and the representativeness in activity and cost, including Cellic CTec 2.0 [kindly donated by Novozymes (China), Beijing, China], Vland LLC 4 (purchased Vland Biotech, Qingdao, China), and # 7 (purchased from an industrial enzyme maker). CTec 2.0 and LLC 4 are liquid enzymes, and # 7 is solid enzyme. The liquid enzyme was taken as water and the mass of the total liquid of the saccharification process was calculated. The # 7 enzyme is the solid enzyme produced by the adsorption of the liquid enzyme onto the solid bran particles and dried for the purpose of long-term storage. There is no need for the extraction step because the bran is hydrolyzed very quickly when the enzyme is put into the hydrolysis system and the cellulase enzyme adsorbed on the bran is releases into the hydrolysate. The filter paper activity was determined according to the NREL protocol LAP-006 (Adney and Baker 1996). The cellobiase activity was determined using the method of Ghose (1987). The total protein concentration was determined by Bradford method using bovine serum albumin (BSA) as protein standard (Bradford 1976). The cellulase enzyme was used based on the total protein weight per gram of cellulose substrate in the biomass feedstock.
The reagents KH2PO4, (NH4)2SO4, MgSO4, and H2SO4 were purchased from Lingfeng chemical reagent, Shanghai, China. Yeast extract was procured from Angel Yeast Co., Yichang, Hubei, China. Agar was purchased from Aladdin BioChem, Shanghai, China.
Strains and medium
Biodetoxification fungus Amorphotheca resinae ZN1 was isolated in our previous works and stored in China General Microorganism Collection Center (CGMCC), Beijing, China with the registration number 7452 (Zhang et al. 2010). A. resinae ZN1 was maintained on a potato dextrose agar medium (PDA) slant. The PDA medium was prepared by boiling 200 g of peeled and sliced potatoes in 1 L deionized water for 30 min. 15 g/L of agar was added for preparation of PDA slant for A. resinae ZN1 growth.
Ethanol fermentation strain Saccharomyces cerevisiae XH7 was an engineered strain from the wild diploid Saccharomyces cerevisiae BSIF (Li et al. 2015). The strain was cultured in YPD medium containing 20 g/L of glucose, 20 g/L of peptone, and 10 g/L of yeast extract. The culture vial was stored in the YPD medium containing 30% of glycerol at −80 °C freezer.
The media used included (1) activation medium, 20 g/L of glucose, 20 g/L of peptone, 10 g/L of yeast extract; (2) seed culture medium, 5% (w/w) of the pretreated and biodetoxified corn stover, the cellulase dosage of 10 mg protein per gram of cellulose, 2 g/L of KH2PO4, 2 g/L of (NH4)2SO4, 1 g/L of MgSO4, 10 g/L of yeast extract; (3) adaptation seed medium, 10% (w/w) of the pretreated and biodetoxified corn stover, the cellulase dosage of 10 mg protein per gram of cellulose, 2 g/L of KH2PO4, 2 g/L of (NH4)2SO4, 1 g/L of MgSO4, 10 g/L of yeast extract. The seed culture medium contained only low concentration of xylose from the pretreated corn stover feedstock and no glucose or pre-hydrolysate in it at the beginning of the culture. As the seed culture proceeds, the added pretreated and detoxified corn stover is hydrolyzed into soluble glucose by the cellulase, and the glucose is acting as the carbon source for the seed cell growth. In this way, the pure glucose sugar is saved by corn stover feedstock; and (4) SSCF medium, 2 g/L of KH2PO4, 2 g/L of (NH4)2SO4, 1 g/L of MgSO4, 10 g/L of yeast extract.
Pretreatment, biodetoxification, and SSCF
Corn stover was pretreated using the dry dilute acid pretreatment (DDAP) method (Zhang et al. 2011; He et al. 2014). The major components’ contents and the inhibitors’ contents in the pretreated biomass feedstocks were determined according to NREL protocols (Sluiter et al. 2008, 2012). The pretreated biomass was briefly disk milled to remove the long cellulose fibers to avoid the blockage of the slurry flow of the downstream hydrolysate and broth.
The pretreated biomass solids were biodetoxified in a 15-L bioreactor at 28 °C and aeration for 36 h to remove the inhibitors generated during the dry dilute acid pretreatment operation (Zhang et al. 2010; He et al. 2016).
The pretreated solids were firstly converted into liquid hydrolysate slurry containing both monosaccharides (glucose and xylose) and oligomer sugars (oligo-glucan and oligo-xylan) in the specially designed 5 L bioreactors equipped with helical ribbon impeller (Zhang et al. 2011) at 50 °C, pH 4.8 for 12 h. Then glucose and xylose were co-fermented into ethanol simultaneously with the further hydrolysis of cellulose and oligomer sugars (simultaneous saccharification and co-fermentation, SSCF) by the engineered Saccharomyces cerevisiae XH7 at the high solids loading (30%, w/w) in the same bioreactor at 30 °C for 96 h by inoculating the shortly adapted yeast seed cells into the hydrolysate at 10% (v/v). The nutrients added included 2 g/L of KH2PO4, 2 g/L of (NH4)2SO4, 1 g/L of MgSO4, 10 g/L of yeast extract. Samples were periodically withdrawn and for analysis of glucose, xylose, ethanol, glycerol, acetic acid, furfural, and 5-hydroxymethylfurfural (HMF).
The S. cerevisiae XH7 seed broth was prepared in a two-step adaption procedure using the pretreated biomass feedstock as the carbon source instead of glucose sugar (Qureshi et al. 2015).
Calculation of ethanol yield
Xylose conversion is calculated by measuring the percentage ratio of the decreased xylose concentrations in the hydrolysate at the beginning and the end of the SSCF operation over the total xylose concentration.
Sugars, ethanol, acetic acid, 5-HMF, Furfural, and Glycerol were analyzed on HPLC (LC-20AD, Shimazu, Kyoto, Japan) equipped with a Bio-rad Aminex HPX-87H column (Bio-rad, Hercules, CA, USA) and RID-10A detector (Shimadzu, Kyoto, Japan). 5 mM H2SO4 solution was used as flow phase at the flow rate of 0.6 mL/min. Furans were analyzed on HPLC (LC-20AT, Shimazu, Kyoto, Japan) equipped with a YMC-Pack ODS-A column (YMC, Tokyo, Japan) and an SPD-20A UV detector (Shimadzu, Kyoto, Japan).
The yeast cell viability in the simultaneous saccharification and co-fermentation (SSCF) was assayed by counting the colony-forming units (CFU) on the YPD (Gu et al. 2015) petri dish when the 100 μL of the 10−5 or 10−6 diluted fermentation broth withdrawn at different time points were stretched and cultured for 48 h at 30 °C.
Results and discussion
Enzyme assays of filter paper unit, cellobiase activity, and total protein content
Activity assays of the industrial cellulase enzymes
Cellic CTec 2.0
Vland LLC 4
Total protein content (mg/mL or mg/g)
Filter paper unit (FPU/mL or FPU/g)
β-glucosidase unit (CBU/mL or CBU/g)
FPU and CBU ratio (FPU/CBU)
Specific filter paper unit (FPU/mg protein)
SSCF assay under the same cellulase protein additions
SSCF of corn stover using different industrial cellulase enzymes
Ethanol titer (g/L)
Ethanol yield (%)a
Xylose conversion (%)
Cellic CTec 2.0
Valnd LLC 4
The 12-h pre-hydrolysis of 30% (w/w) solid content system generated 82.4, 74.3, and 63.6 g/L of glucose by CTec 2.0, LLC 4, and # 7, respectively. The hydrolysis result indicates that the hydrolysis capacity of CTec 2.0 is advantage to LLC 4 and # 7. The 96-h SSCF generated 76.3, 73.0, 76.0 g/L of ethanol and 73.8, 73.7, 76.4% of conversion yields by CTec 2.0, LLC 4, and # 7, respectively. Similar ethanol titer and yield were obtained in the given cellulase dosage (10 mg protein per gram of cellulose), although the considerable difference in hydrolysis capacity existed. The SSCF results indicate that the all the three cellulase worked well in the SSCF to achieve the high ethanol titer and yield, but certain differences existed. The xylose conversions achieved were 83.4, 85.6, and 89.5%, respectively. when CTec 2.0, LLC 4, and # 7 were used. The cell viability result shows that the lower cellulose conversion and glucose accumulation by # 7 led to the better cell growth of the fermenting yeast cells, while CTec 2.0 and LLC 4 with the high hydrolysis yields did not help in making the xylose conversion. Glycerol formation accumulated to about 12 g/L and considerably reduced the ethanol yield, revealing that the fermenting yeast was under the stress of high glucose concentration then easily led to the glycerol formation.
Cellulase enzymes may also contain some soluble carbohydrates (Zhang et al. 2007), which can be directly used for ethanol production in SSCF. Three industrial cellulases, CTec 2.0, LLC 4, and # 7, contained 277.1, 13.4, and 12.9 mg/g of glucose, respectively, as well as 36.2, 4.4, and 0.9 mg/g of xylose. At 30% solids loading, and with the cellulase dosage of 10 mg protein per gram of cellulose, the three enzymes would provide 4.88, 0.32, and 0.40 g/L of carbohydrates (including glucose and xylose) which theoretically generated 2.5, 0.16, and 0.20 g/L of ethanol, individually. Compared with the other two enzymes, CTec 2.0 supplied more fermentable sugars for SSCF. However, the ethanol obtained from the sugars was quite lower, and it was difficult to calculate it accurately in practice. As a result, the effect of the carbohydrates from the cellulase on the ethanol production was not considered in this study.
SSCF assays under varying cellulase enzyme dosage
The 12-h pre-hydrolysis assay shows the similar tendency at varying cellulase dosages. The hydrolysis capacity of CTec 2.0 showed the maximum hydrolysis yield at each cellulase dosage from 5 to 25 mg/g, followed by the LLC 4 and then # 7. The hydrolysis yield increased with the increasing cellulase dosage but the increase almost ceased or slowed down due to the increasing glucose inhibition on the cellulase enzyme activity. When the cellulase dosage was in the range of 5–10 mg protein per gram of cellulose, the glucose concentrations increased by 66, 21, and 17% with the use of # 7, CTec 2.0, and LLC 4, respectively. When the cellulase dosage was in the range of 10–15 mg protein per gram of cellulase, the glucose concentration increased by 14, 11, and 12%, respectively. When the cellulase dosage was in the range of 15–25 mg protein per gram of cellulose, the glucose concentrations only increased by 7 and 10% by CTec 2.0 and LLC 4, respectively, while # 7 did not show the increase in glucose concentration. The xylose utilization by # 7 was the optimal because of the low glucose concentration provided.
The SSCF assay shows that the ethanol titer and yield from the SSCF by CTec 2.0, LLC 4, and # 7 were close (about 80 g/L) when the cellulase dosage was in the higher range of 10, 15, 25 mg protein per gram of cellulose, indicating the higher overdose of cellulase enzyme did not help in further improvement of ethanol titer and yield. High cellulase dosage led to the high glucose concentration in the pre-hydrolysis step, and the high glucose inhibited the cell growth and conversion rate of glucose and xylose to ethanol. However, the minimum dosage of cellulase (5 mg protein per gram of cellulose) showed the differences in the ethanol titer and yield by CTec 2.0, LLC 4, and # 7 were significantly different: the 96-h SSCF generated 68.1, 68.7, 56.1 g/L of ethanol and 66.6, 69.0, 49.8% of conversion yields by CTec 2.0, LLC 4, and # 7, respectively. The ethanol titer and yield by # 7 were relatively lower at the minimum dosage of cellulose. As shown in Fig. 2c, d, the activities of filter paper unit (FPU) and cellobiose (CBU) of # 7 were much lower than those of CTec 2.0 and LLC 4 at the same cellulase dosage, especially in the minimum range, which inevitably led to lower hydrolysis yield, ethanol titer, and ethanol yield by # 7.
Based on the SSCF results at the 10 mg protein per gram of cellulose, for producing 1 kg of cellulosic ethanol, 21.6 g of cellulase protein of CTec 2.0, equivalent to 247 g of the liquid enzyme; or 20.9 g cellulase protein of LLC 4, equivalent to 275 g of the liquid enzyme; or 21.3 g of cellulase protein of # 7, equivalent to 457 g of the solid enzyme, is needed. If the cellulase enzyme is based on the same price per kilogram enzyme by volume or weight, then CTec 2.0 is the least expensive. However, if the enzyme is sold based on the total proteins of the enzyme product, the cost of the enzymes is similar for the three enzymes.
The industrial cellulase enzymes shows significantly different performances in activity and cellulose hydrolysis yield, and less significant ethanol titer and yield based on the total protein dosage per gram of cellulose of corn stover. In general, the industrial enzymes available as cellulase products in the market give satisfactory performance and can be applied for the practical cellulosic ethanol production on a commercial scale.
QZ and JB designed and wrote the experiment; QZ conducted the experiment; JB conceived the research. Both authors read and approved the final manuscript.
The authors declare that they have no competing interests.
Availability of data and materials
The datasets supporting the conclusions of this article are included in the main manuscript file.
Ethics approval, consent to participate, and consent for publication
All authors have read and approved the manuscript before submitting it to bioresources and bioprocessing. There is no competing interests to declare by any author in relation to the submission.
This research was supported by the funding granted to JB by the National High-Tech Program of China (2014AA021901).
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- Adney B, Baker J (1996) Measurement of cellulase activities. AP-006. NREL. Analytical Procedure. National Renewable Energy Laboratory, Golden COGoogle Scholar
- Bradford MM (1976) A rapid and sensitive method for the quantitation of microgram quantities of protein utilizing the principle of protein-dye binding. Anal Biochem 72:248–254View ArticleGoogle Scholar
- Chen XW, Kuhn E, Jennings EW, Nelson R, Tao L, Zhang M (2016) DMR (deacetylation and mechanical refining) processing of corn stover achieves high monomeric sugar concentrations (230 g/L) during enzymatic hydrolysis and high ethanol concentrations (>10% v/v) during fermentation without hydrolysate purification or concentration. Energy Environ Sci 9:1237–1245View ArticleGoogle Scholar
- Chiaramonti D, Balan V, Kumar S (2013) Review of US and EU initiatives toward development, demonstration, and commercialization of lignocellulosic biofuels. Biofuels Bioprod Bioref 7:732–759View ArticleGoogle Scholar
- Gang L, Jian Z, Jie B (2016) Cost evaluation of cellulase enzyme for industrial-scale cellulosic ethanol production based on rigorous aspen plus modeling. Bioprocess Biosyst Eng 39:133–140View ArticleGoogle Scholar
- Ghose TK (1987) Measurement of cellulase activities. Pure Appl Chem 59:257–268Google Scholar
- Gu HQ, Zhang J, Bao J (2015) High tolerance and physiological mechanism of zymomonas mobilis to phenolic inhibitors in ethanol fermentation of corncob residue. Biotechnol Bioeng 112:1770–1782View ArticleGoogle Scholar
- He Y, Zhang J, Bao J (2014) Dry dilute acid pretreatment by co-currently feeding of corn stover feedstock and dilute acid solution without impregnation. Bioresour Technol 158:360–364View ArticleGoogle Scholar
- He Y, Zhang J, Bao J (2016) Acceleration of biodetoxification on dilute acid pretreated lignocellulose feedstock by aeration and the consequent ethanol fermentation evaluation. Biotechnol Biofuels 9:19View ArticleGoogle Scholar
- Klein-Marcuschamer D, Oleskowicz-Popiel P, Simmons BA, Blanch HW (2012) The challenge of enzyme cost in the production of lignocellulosic biofuels. Biotechnol Bioeng 109:1083–1087View ArticleGoogle Scholar
- Lei C, Zhang J, Xiao L, Bao J (2014) An alternative feedstock of corn meal for industrial fuel ethanol production: delignified corncob residue. Bioresour Technol 167:555–559View ArticleGoogle Scholar
- Li H, Wu M, Xu L, Jin H, Guo T, Bao X (2015) Evaluation of industrial saccharomyces cerevisiae strains as the chassis cell for second-generation bioethanol production. Microb Biotechnol 82:66Google Scholar
- Liu S, Wang Q (2014) Response surface optimization of enzymatic hydrolysis process of wet oxidation pretreated wood pulp waste. Cellul Chem Technol 50:803–809Google Scholar
- Marcos M, González-Benito G, Coca M, Bolado S, Lucas S (2013) Optimization of the enzymatic hydrolysis conditions of steam-exploded wheat straw for maximum glucose and xylose recovery. J Chem Technol Biotechnol 88:237–246View ArticleGoogle Scholar
- Qureshi AS, Zhang J, Bao J (2015) High ethanol fermentation performance of the dry dilute acid pretreated corn stover by an evolutionarily adapted saccharomyces cerevisiae, strain. Bioresour Technol 189:399–404View ArticleGoogle Scholar
- Ramesh D (2013) World’s first commercial scale cellulosic biofuels plant opens. Chem Week 175:39Google Scholar
- Sluiter A, Hames B, Ruiz R Scarlata C, Sluiter J Templeton D (2008) Determination of sugars, byproducts, and degradation products in liquid fraction process samples. NREL/TP-510-42623. National Renewable Energy Laboratory, Golden COGoogle Scholar
- Sluiter A, Hames B, Ruiz R, Scarlata C, Sluiter J, Templeton D, Crocker D (2012) Determination of structural carbohydrates and lignin in biomass. NREL/TP-510-42618. National Renewable Energy Laboratory, Golden COGoogle Scholar
- Zhang J, Bao J (2012) A modified method for calculating practical ethanol yield at high lignocellulosic solids content and high ethanol titer. Bioresour Technol 116:74–79View ArticleGoogle Scholar
- Zhang Y, Schell D, Mcmillan J (2007) Methodological analysis for determination of enzymatic digestibility of cellulosic materials. Biotechnol Bioeng 96:188–194View ArticleGoogle Scholar
- Zhang J, Zhu Z, Wang X, Wang N, Wang W, Bao J (2010a) Biodetoxification of toxins generated from lignocellulose pretreatment using a newly isolated fungus Amorphotheca resinae ZN1 and the consequent ethanol fermentation. Biotechnol Biofuels 3:26View ArticleGoogle Scholar
- Zhang J, Chu D, Huang J, Yu Z, Dai G, Bao J (2010b) Simultaneous saccharification and ethanol fermentation at high corn stover solids loading in a helical stirring bioreactor. Biotechnol Bioeng 105:718–728Google Scholar
- Zhang J, Wang X, Chu D, He Y, Bao J (2011) Dry pretreatment of lignocellulose with extremely low steam and water usage for bioethanol production. Bioresour Technol 102:4480–4488View ArticleGoogle Scholar
- Zhang J, Shao S, Bao J (2015) Long term storage of dilute acid pretreated corn stover feedstock and ethanol fermentability evaluation. Bioresour Technol 201:355–359View ArticleGoogle Scholar
- Zhang H, Han X, Wei C, Bao J (2016) Oxidative production of xylonic acid using xylose in distillation stillage of cellulosic ethanol fermentation broth by gluconobacter oxydans. Bioresour Technol 224:573–580View ArticleGoogle Scholar