Prefermentation improves ethanol yield in separate hydrolysis and cofermentation of steam-pretreated wheat straw
© The Author(s) 2016
Received: 13 April 2016
Accepted: 7 June 2016
Published: 1 July 2016
Agricultural residues, such as wheat straw, are feasible substrates for ethanol fermentation provided that pentoses and hexoses can be converted efficiently. Separate hydrolysis and cofermentation (SHCF) constitute a framework for improvement of conversion efficiency, because it permits independent optimization of the enzymatic hydrolysis and cofermentation steps. A drawback is that the high glucose concentrations present in SHCF repress xylose utilization and constrain ethanol yields. To improve xylose utilization the xylose-rich hydrolyzate liquor was separated from glucose-rich solids and the phases were cofermented sequentially. Prefermentation of the xylose-rich hydrolyzate liquor followed by fed-batch cofermentation of glucose-rich prehydrolyzed solids enabled sequential targeting of xylose and glucose conversion. The aim was to improve the xylose conversion by lowering the glucose repression of the xylose uptake. Various prefermentation configurations and feed patterns for prehydrolyzed solids were examined. Prefermentation increased ethanol yields overall, and fed-batch prefermentation reduced xylitol production. The best results were obtained by balancing promotion of efficient xylose conversion with maintained yeast viability. Fed-batch prefermentation and a single addition of prehydrolyzed solids, elicited an ethanol yield of 0.423 g·g−1 and a xylitol yield of 0.036 g·g−1.
KeywordsSaccharomyces Cerevisiae Xylose Cofermentation Prefermentation Prehydrolysis Lignocellulose Ethanol
Fermentative conversion of lignocellulosic biomass into ethanol provides a sustainable alternative that could partially replace traditional petroleum refining, but to successfully implement lignocellulosic technologies economic sustainability must be ensured. High final ethanol concentration and high ethanol yield has been identified as key factors for improved process economics . To achieve these, efficient hydrolysis and fermentation as well as utilization of a variety of sugars present in the feedstock are necessary.
The main obstacles to efficient cofermentation of lignocellulose-derived sugars are the limitations of the microbial physiology that restricts efficient conversion of various substrates  and the ability to cope with a variety of inhibitors . The wild-type strain of Saccharomyces cerevisiae is tolerant to many inhibitors that are generated by thermochemical pretreatment, but it is largely unable to convert pentoses into ethanol without genetic modification . Exogenous genes that encode for xylose reductase (XR) and xylitol dehydrogenase (XDH) [5, 6], as well as xylose isomerase , have been introduced into the S. cerevisiae genome to enable assimilation of xylose. However, fermentation of xylose to ethanol by engineered S. cerevisiae is slower and generally results in lower ethanol yields than glucose fermentation . This is likely because of limitations in capacity in the pentose phosphate shunt  and an imbalance in redox cofactors in engineered XR/XDH-pathways . The cofactor imbalance between the NAD(P)H-consuming XR and NADH-producing XDH catalyzed reactions restricts flux through the engineered pathway, and causes xylitol production [11, 12]. Improvements have been made by altering the cofactor specificity of XR towards NADH [13, 14], and by overexpression of endogenous xylulokinase . However, the distribution of products and the rate of conversion remain dependent on the balance and turnover of cofactors. The xylose conversion capacity, as well as tolerance of inhibitors, have been further improved in engineered S. cerevisiae strains by evolutionary engineering and adaptation strategies , but the slow cellular uptake of pentoses remains a constraint for efficient xylose conversion. Xylose is taken up by nonspecific hexose transport mechanisms , and because their affinity for glucose is many-fold higher than for xylose  excessive amounts of glucose competitively inhibit the transporters and prevent efficient uptake of xylose. However, low concentrations of glucose have been shown to enhance the xylose uptake rate , which imply coconsumption . The enhanced xylose uptake rate has been attributed to improved cofactor recycling , and the induction of genes expression for transporter systems  and glycolytic enzymes .
Fermentation design can provide a tool to improve xylose utilization and conversion efficiency by accommodating the substrate consumption patterns of the fermenting microorganism. Thus, various strategies have been proposed to optimize the conversion of biomass-derived glucose and xylose to ethanol, where enzymatic hydrolysis and fermentative conversion can be performed either sequentially (separate hydrolysis and cofermentation, or SHCF) or simultaneously in a single vessel (simultaneous saccharification and cofermentation, or SSCF). Opting for either strategy is generally a trade-off between optimal temperatures and inhibitory glucose concentrations during hydrolysis on the one hand (SHCF) and suboptimal temperatures and ethanol-inhibited cellulolysis on the other (SSCF). Whereas some studies have shown that SSCF-based designs generally result in higher yields [18, 21], the separate hydrolysis in SHCF-based designs enable optimization of the process conditions in the individual steps. Performing separate hydrolysis eliminates rate limiting effects of the hydrolysis on conversion rates, and problems associated with high viscosity during fermentation are alleviated by prior liquefaction of the solids. These properties become increasingly important as the solids load is increased in the process. Both strategies have advantages, and the choice is strain and feedstock dependent. Modifications to the fundamental strategies have been implemented to improve fermentation performance and substrate utilization [22–24]. Fed-batch design has been implemented to promote coconsumption in SHCF [22, 23]. Fed-batch designs, where a glucose-rich feed supported the xylose utilization, improved the overall ethanol yields, and lowered xylitol production in co-fermentation of steam-pretreated wheat straw with strains of xylose-fermenting S. cerevisiae . Further, prefermentation has been implemented as a modification to SSCF to improve xylose utilization and ethanol yields [24, 25]. Depletion of glucose in the liquid fraction of whole spruce slurry, prior to enzyme addition in SSCF, reduced the competitive inhibition of the xylose uptake and increased ethanol yields . The authors presupposed that the process significance would be even greater with xylose-rich feedstocks. When pretreated agricultural residues are used as substrate, which have higher xylose content than spruce, the use of prefermentation can be extended to encompass substantial xylose conversion. The high xylose concentration, in combination with low glucose concentration, in the hydrolyzate liquor provide glucose-to xylose ratios during prefermentation that kinetically favor xylose uptake . By separating the hydrolyzate liquor from the lignocellulosic solids, the advantages of an SHCF strategy can be combined with the beneficial conditions for xylose conversion in prefermentation. The combined strategy features sequential targeting of xylose and glucose conversion with optimal temperatures and customization of the enzymatic hydrolysis and fermentation steps individually. It has previously been demonstrated with a 2-step batch-SSCF of AFEX-pretreated switchgrass that sequential targeting of xylose and glucose conversion improve xylose utilization and ethanol yields .
In this study, various SHCF-based cofermentation strategies for the conversion of glucose and xylose to ethanol were examined. Two wheat straw slurries with various inhibitor concentrations, prepared by dilute acid catalyzed steam-explosion, were used. The pentose-rich hydrolyzate liquor in the slurries was separated from the hexose-rich solids to enable sequential targeting of xylose and glucose conversion. Cofermentation was performed by a xylose-fermenting and inhibitor tolerant strain of S. cerevisiae in a 2-step process, where prefermentation of the hydrolyzate liquor was followed by feeding of enzymatic hydrolysate, which consisted of prehydrolyzed unwashed solids. The hypothesis was that xylose could be converted with greater efficiency and render higher ethanol yields under the more favorable conditions for xylose conversion in the sequential fermentation steps than by conventional SHCF. Various feed patterns during prefermentation and for the addition of enzymatic hydrolyzate were examined to improve the xylose conversion and maximize the ethanol yield.
Fermentation was performed with the non-commercial recombinant Saccharomyces cerevisiae KE6-12 strain (Taurus Energy AB), which harbors genes from Scheffersomyces stipitis (formerly Pichia stipitis) that encode for xylose reductase (XR) and xylitol dehydrogenase (XDH) and overexpressing endogenous xylulokinase (XK), thus enabling xylose conversion. The strain was developed by evolutionary engineering  on the industrial strain S. cerevisiae TMB3400  to improve inhibitor tolerance and xylose conversion capacity. Stock culture aliquots contained a mass fraction of 20 % glycerol in water and were stored at −80 °C.
Raw material and preprocessing
Two batches of wheat straw that were pretreated with dilute acid-catalyzed steam explosion under various conditions were procured from SEKAB E-Technology AB (Örnsköldsvik, Sweden). The slurries were denoted severe or mild slurry, respectively, based on the relative inhibitor concentrations in the hydrolyzate liquor. The severe slurry was prepared by impregnation with dilute H2SO4, pH 2.4, and steam-pretreatment at 190 °C for 15 min, and had a water-insoluble solids (WIS) content of 13.9 wt % and a total dry-matter (DM) content of 20.1 wt %. The mild slurry was prepared by impregnation of wheat straw with dilute H2SO4, pH 1.7, and steam-pretreatment at 187 °C for 8 min, and had a WIS content in the range of 11.1–12.7 wt % and a total DM content in the range of 17.5–18.2 wt %. The pH of the slurries was adjusted to 5 with 12.5 M NaOH, and the hydrolyzate liquor was separated from the solids by filtration using a hydraulic press (HP5 M, Fischer Maschinenfabrik). The unwashed solid fraction of the severe slurry had a WIS content of 34 wt % after filtration, versus between 38 and 44 wt % WIS in the unwashed solid fraction of the mild slurry.
Cultivation of yeast
The precultures were cultivated in 250 ml shake flasks with 150 ml of sterile minimal medium, containing 20 g·L−1 glucose, 20 g·L−1 xylose, 7.5 g·L−1 (NH4)2SO4, 3.75 g·L−1 KH2PO4, and 0.75 g·L−1 MgSO4 7 H2O. The media was supplemented with 1 mL·L−1 vitamin solution and 10 mL·L−1 trace element solution, per Taherzadeh et al. . The pH of the medium was adjusted to 5.5 with 5 M NaOH in all precultures, all of which were inoculated with 300 µl of the stock cell aliquots. The preculture was incubated at 30 °C on an orbital shaker (Lab-Therm, Kühner) at 180 rpm for 24 h.
The cultivations were performed in a sterilized 2 L Labfors bioreactor (Infors AG) equipped with two six-blade Rushton turbines. The reactor diameter to impeller diameter ratio was 3, and the reactor height to diameter ratio was 1.7. The yeast was propagated with aerobic batch cultivation on molasses followed by aerobic fed-batch cultivation on wheat straw hydrolyzate liquor and molasses. The batch cultivation was performed with 50 g·L−1 molasses solution that was supplemented with 23.5 g·L−1 (NH4)2SO4, 3 g·L−1 KH2PO4, 2.25 g·L−1 MgSO4 ·7 H2O, 33 µg·L−1 biotin, and 120 ppm Vitahop (BetaTec). The molasses (Nordic Sugar A/S) contained 40 wt % fermentable sugars (sucrose, fructose, and glucose), lactic acid (0.034 g·g−1), and acetic acid (0.008 g·g−1). The cultivation was initiated by inoculation with the preculture. The batch cultivation was performed with 0.5 L working volume, with a constant aeration rate of 1 vvm, pH maintained at 5.2 and an agitation rate of 700 rpm. The batch phase was concluded when all sugars were consumed, as indicated by the evolution of carbon dioxide and oxygen in the bioreactor gas effluent.
The fed-batch phase was initiated after fermentable sugars were depleted in the batch phase. The feed solution comprised diluted wheat straw hydrolyzate liquor that was supplemented with 150 g·L−1 of molasses. The hydrolyzate liquor in the feed solution brought about inhibitor concentrations in the final working volume that corresponded to the concentrations in a broth with a 7.5 wt % WIS load. The purpose of the hydrolyzate liquor in the fed-batch phase was to improve yeast tolerance by short-term adaptation of the cultivated yeast to the environmental conditions in the fermentation experiments, per Nielsen et al. . The feed solution was pulse-fed to the bioreactor at a constant rate for 20 h to a final working volume of 1.5 L. The reactor was aerated by sparging at a constant rate of 1 vvm, based on the final volume, and the pH was maintained at 5.2 automatically with sterile 2.5 M NaOH solution.
The propagated yeast was harvested by centrifugation (3800×g, 10 min) and washed with 9 g·L−1 sterile NaCl solution. The cell pellets were resuspended in sterile 9 g·L−1 NaCl solution to yield inocula with a cell dry matter concentration of 120 g·L−1.
Enzymatic hydrolysis of the solid fractions
Separate hydrolysis and cofermentation
All cofermentations were performed in sterilized 2 L Labfors bioreactors (Infors AG) equipped with an anchor impeller and a pitched six-blade turbine. The reactor diameter to impeller diameter ratio was 1.5 for the anchor impeller and 1.7 for the pitched six-blade turbine, and the reactor height to diameter ratio was 1.7. All cofermentations were supplemented with 0.5 g·L−1 (NH4)2HPO4, 0.125 mL·L−1 Vitahop (BetaTec), and 0.4 mL·L−1 Antifoam RD Emulsion (Dow Corning), all based on the final volume. The pH in the fermentation broths were maintained at 5.2 by automatic addition of sterile 2.5 M NaOH solution.
SHCF with prefermentation
The prefermentation of hydrolyzate liquor followed by fed-batch cofermentation of enzymatic hydrolyzate was performed with a final working weight of 1.5 kg; a total WIS load of 10 wt %, based on the final weight; a yeast load of 5 g·L−1 of dry matter (DM), based on the final volume; and an overall enzyme load of 10 FPU·g−1 WIS.
The fermentations were performed sequentially by prefermentation of the hydrolyzate liquor, followed by cofermentation of the enzymatic hydrolyzate (Fig. 1). The prefermentation of the hydrolyzate liquor was performed using either of two feed strategies: batch or fed-batch. In batch prefermentation, the entire amount of separated hydrolyzate liquor was supplied at outset and cofermented for 48 h. For fed-batch prefermentation, a two-step process was adopted. Approximately 25 wt % of the separated hydrolyzate liquor was cofermented in batch for 12 h, and the remaining 75 wt % was fed linearly to the fermentor for the subsequent 36 h. The amount of hydrolyzate liquor at outset was set to surpass minimum required liquid level in the fermentor (≥200 mL) to ensure reliable pH and temperature control. Regardless of mode, the full yeast load, 5 g·L−1, was pitched at outset and 1 FPU·g−1 WIS of Cellic CTec2, based on total ingoing WIS, was added after 4 h to hydrolyze solubilized oligosaccharides. The hydrolyzate liquor was cofermented under anaerobic conditions at 30 °C for 48 h, and the bioreactor was agitated at 300 rpm.
Two feed strategies were used for the following fed-batch cofermentation of the enzymatic hydrolyzate: (i) all enzymatic hydrolysate was added after 48 h, and (ii) half of the enzymatic hydrolyzate was added after 48 h, and the remaining half added after 72 h. Enzymes, equivalent to a total enzymatic activity of 9 FPU·g−1 WIS, were carried over with the addition of enzymatic hydrolyzate, resulting in total cellulolytic activity of 10 FPU·g−1 WIS, based on the total ingoing WIS content. The temperature was maintained at 30 °C, and agitation was maintained at 300 rpm. The experiments were terminated after a total fermentation time of 144 h.
Model cofermentations were performed with a final working weight of ~1.4 kg using mild and severe hydrolyzate liquor from the pretreated wheat straw slurries. The hydrolyzate liquor was diluted with distilled water to inhibitor and sugar concentrations that corresponded to a WIS load of 10 wt %. Further, the hydrolyzate liquor was supplemented with glucose, corresponding to 81 % yield in enzymatic hydrolysis of the solid fraction. The supplemented hydrolyzate liquor mimicked the composition of enzymatically hydrolyzed slurry. An enzyme load of 2 FPU·g−1 WIS was applied to hydrolyze solubilized oligosaccharides, and the fermentor was inoculated with a yeast load of 5 g·L−1 DM. All components were added at the outset. The model cofermentation mimicked a batch SHCF, but avoided the bias from influence of solid material and hydrolysis limitations in the cofermentation. The hydrolyzate liquor was cofermented under anaerobic conditions at 30 °C for 144 h, and the bioreactor was agitated at 300 rpm.
Extracellular metabolites, inhibitors, and sugars were measured by high-performance liquid chromatography (HPLC) on a Shimadzu HPLC system that was equipped with an RID-10A refractive index detector (Shimadzu). Samples for carbohydrate analysis with low pH (from hydrolyzate liquors) were adjusted to pH 5 with CaCO3 and centrifuged in 10 mL tubes (960×g, 5 min). All samples were centrifuged (16,000×g, 3 min), and the supernatants filtered through 0.20 μm syringe filters (GVS Filter Technology). Filtered samples were stored at −20 °C until analysis.
Extracellular metabolites, organic acids, and degradation products in the hydrolyzate liquors and fermentation broth were analyzed by isocratic ion-exchange chromatography using an Aminex HPX-87H column (Bio-Rad Laboratories) at 50 °C. The eluent was 5 mM H2SO4, applied at a flow rate of 0.5 mL·min−1. Sugars and xylitol in the hydrolyzate liquors and fermentation broth were quantified by isocratic ion-exchange chromatography on an Aminex HPX-87P column (Bio-Rad Laboratories) at 85 °C. Deionized water was used as the eluent at a flow rate of 0.5 mL·min−1.
Dry matter content (DM) of solids and water-insoluble solids (WIS) were measured per Sluiter et al. , and Sluiter et al. , respectively. Soluble carbohydrates, monomeric sugars that were released into solution during pretreatment, and pretreatment degradation products were quantified by acid hydrolysis and HPLC per Sluiter et al. . Further, structural carbohydrates, lignin, and ash contents of the water-insoluble fraction of the wheat straw slurries were measured per Sluiter et al. .
Calculation of yields
Ethanol yields were calculated at two levels: an overall yield and a metabolic yield. The overall ethanol yield was based on total supplied glucose and xylose; i.e. the sum of glucose and xylose present in the slurries, including monomers, oligomers, and polymers. The metabolic ethanol yield was based on consumed glucose and xylose. The mass of glucose and xylose available in the form of polymers in the WIS were corrected with factors 1.111 and 1.136, respectively, to account for the addition of water to the monomeric units during hydrolysis. The percentage of maximum theoretical ethanol yield was based on a theoretical stoichiometric yield of 0.51 g·g−1 on glucose and xylose.
Results and discussion
Material preprocessing and composition
Composition of structural carbohydrates and lignin in the water-insoluble fractions of the pretreated materials and sugar compositions and prevalence of inhibitory compounds in hydrolyzate liquors
Severe wheat straw slurry
Mild wheat straw slurry
Steam-pretreated material (% of dry weight)
Hydrolyzate liquor (g·L−1)
The separation of hydrolyzate liquors from the lignocellulosic solids by filtration, in combination with the compositional differences between the phases (Table 1), enabled the sequential targeting of xylose and glucose conversion. The hydrolyzate liquor contained most of the xylose and inhibitors and the unwashed lignocellulosic solids harbored mainly cellulose and lignin. This allowed the use of feeding schemes that mitigate the impact of inhibitors and effect more favorable glucose-to-xylose ratios for xylose utilization could be implemented.
Enzymatic hydrolysis of the solid fractions
The enzymatic hydrolysis of the retained solids after filtration was performed at high WIS loads, because of the separation of hydrolyzate liquor from the lignocellulosic solids. The dilution of the solid fractions was further constrained by the intended WIS load of 10 wt % in the SHCF experiments and the aim to maximize separation between the bulk fractions of glucose and xylose.
The unwashed solid fraction of the severe slurry was diluted from a WIS content of 34 wt % in the retained solids to the 20 wt % used in the enzymatic hydrolysis. The unwashed retained solids from the mild slurry was diluted from a WIS content of 44 to the 26 wt % WIS applied in the enzymatic hydrolysis. Sufficient water for dilution was available to provide even distribution of enzyme preparation and sufficient mixing. Liquefaction became apparent after a few hours, and an extensive degradation of solids occurred during the enzymatic hydrolysis. The enzymatic hydrolysis was performed to produce a glucose-rich enzymatic hydrolysate, and not evaluated further.
Performing the enzymatic hydrolyses at high WIS loads imply the risk of lower sugar yields in hydrolysis. It has been shown for several lignocellulosic substrates that greater substrate loads decrease the corresponding hydrolysis yield . The effect has been attributed to product inhibition [36, 37], inhibition by sugar-derived inhibitors and lignin [38, 39], and mass transfer limitations and other effects that are related to the increased WIS loads . However, inhibition primarily affects the hydrolysis rate— not the maximum conversion or yield—given sufficient time. Minor inefficiencies in the hydrolysis could be rectified with the employed cofermentation strategy, because the enzymes were carried over from the enzymatic hydrolysis to the subsequent cofermentation step, and provided an additional period of hydrolysis. Despite the possibility to partially rectify hydrolysis inefficiencies obtaining high sugar yields in the hydrolysis was important to successfully carry out the devised SHCF-design.
Strategies for separate hydrolysis and cofermentation
In the first cofermentation step, the prefermentation, xylose conversion was targeted. The prefermentation of the hydrolyzate liquors separated from mild and severe slurry were conducted in batch and fed-batch. In the second cofermentation step, the fed-batch cofermentation, glucose conversion was targeted, and remaining xylose coconsumed. The enzymatic hydrolyzate obtained from the enzymatic hydrolysis of the solid fractions, which contained high amounts of glucose, was fed to the prefermented hydrolyzate liquor. One or two additions of enzymatic hydrolyzate were investigated. The aim was to elucidate the impact of number of additions of enzymatic hydrolyzate, independently and in combination with different prefermentation configurations, on xylose utilization and ethanol yield.
Xylose utilization in batch prefermentation
Batch prefermentation of the separated mild hydrolyzate liquor resulted in depletion of glucose and consumption of 88 % of the xylose. The deviation from the mean in the experiments was less than 1 %. The consumed xylose equaled 69 % of the total available xylose in the used slurry. Batch prefermentation of separated mild hydrolyzate liquor elicited higher xylose utilization than with severe hydrolyzate liquor. The glucose in the severe hydrolyzate liquor was depleted and 77 % of the available xylose in the hydrolyzate was consumed, which equaled 48 % of the total available xylose in the used slurry. The substantial consumption of xylose during batch prefermentation reduced the extent of xylose coconsumption needed after the addition of enzymatic hydrolyzate.
Summary of prefermentation results
Severe wheat straw slurry
Mild wheat straw slurry
Residual sugars and end-products [g·L−1]
Metabolic ethanol yield [g·g−1]a
% of theoretical
Xylose utilization [%]
Xylitol yield [g·g−1]b
Xylose utilization in fed-batch prefermentation
To address the inability to sustain coconsumption of xylose and glucose by liberating glucose from the solubilized oligomers in the hydrolyzate liquors, the fed-batch prefermentation strategy was implemented. The fed-batch layout was intended to continuously supply low amounts of glucose and promote coconsumption. The glucose-to-xylose ratio of the hydrolyzate liquors was such (Table 1) that a low measured glucose concentration in the bioreactor could be maintained with a feed of hydrolyzate liquor (Figs. 2b, d, 3b), which kinetically favored xylose consumption . However, lower xylose utilization was observed with fed-batch prefermentation, as compared with batch, with both hydrolyzate liquors (Table 2). On average 77 and 49 % of xylose available in the mild and severe hydrolyzate liquor, respectively, was consumed; as compared to 88 and 77 %, respectively, in batch. The deviation from the mean in fed-batch prefermentation experiments was less than 3 %. The underlying reason for the lower xylose consumption was that the feed rate of xylose-rich hydrolyzate liquor exceeded the xylose uptake rate. In combination with preferential consumption of glucose, this resulted in the accumulation of xylose during the fed-batch phase of the prefermentation (Figs. 2b, d, 3b). Although lower xylose utilizations were achieved with fed-batch prefermentation, substantial fractions of total available xylose in the slurries were consumed. The consumed xylose in mild and severe hydrolyzate liquor after fed-batch prefermentation corresponded to 60 and 31 %, respectively, of total available xylose.
The lower xylose consumptions in fed-batch prefermentation were mirrored in the obtained ethanol concentrations (Table 2), but did not have a significant effect on the metabolic ethanol yields (Table 2). Metabolic ethanol yields of 0.353 and 0.322 g·g−1 were obtained with fed-batch prefermentation of mild and severe hydrolyzate liquor, respectively, as compared to 0.342 and 0.329 g·g−1 with batch prefermentation. The deviations from the mean metabolic ethanol yields were less than 2 % in all instances. Fed-batch prefermentations were also accompanied with lower xylitol production than batch prefermentation. Batch prefermentation of mild and severe hydrolyzate liquor resulted in xylitol yields of 0.136 and 0.134 g·g−1, respectively, whereas only 0.017 g·g−1 respectively 0.041 g·g−1 were produced in fed-batch prefermentation. The deviations from the mean in batch prefermentation experiments were less than 2 %, and less than 7 % in fed-batch prefermentation experiments. The difference in xylitol production between the prefermentation configurations was attributed to the higher xylose consumption rate in batch prefermentation. High xylose consumption rates create a metabolic bottleneck because of an imbalance of cofactors in engineered XR/XDH-pathways [11, 12], whereas it has been shown that lower consumption rates suppress xylitol production . The lower xylose consumption in fed-batch prefermentation in combination with continuous availability of low concentrations of furaldehydes, which act as external electron sinks for the regeneration of cofactors , likely alleviated the cofactor imbalance.
Effect of prefermentation on overall xylose utilization
The selected feed strategy during prefermentation had several intertwined consequences on fermentation performance during the subsequent fed-batch cofermentation of enzymatic hydrolyzate. The different prefermentation configurations had different impacts on fermentative capacity of the yeast during the fed-batch cofermentation of enzymatic hydrolyzate, which was primarily attributed to changes in the viability.
Comparison of overall cofermentation outcome between batch and fed-batch prefermentation of severe hydrolyzate liquor followed by two additions of enzymatic hydrolyzate (Fig. 3) exemplify the different consequences in a high inhibitor concentration context. Batch prefermentation followed by fed-batch cofermentation of enzymatic hydrolyzate elicited a xylose utilization of 71 % and an overall ethanol yield of 0.381 g·g−1. In contrast, the corresponding strategy with fed-batch prefermentation resulted in low glucose conversion and, seemingly, no xylose consumption after fed-batch prefermentation of severe hydrolyzate liquor (Fig. 3b). Fed-batch prefermentation supplied lower initial concentrations of inhibitors than batch prefermentation, but the continuous feed of hydrolyzate liquor seemingly exhausted the yeast. The continuous feed of inhibitors during fed-batch prefermentation exceeded the detoxification rate, which resulted in the accumulation of non-metabolized furaldehydes (data not shown). The furaldehydes were not fully converted during the sequent fed-batch cofermentation of enzymatic hydrolyzate. In contrast, the yeast was resilient to the higher initial inhibitor concentrations in batch prefermentation. The yeast was capable of promptly detoxifying the hydrolyzate liquor during batch prefermentation and after each addition of enzymatic hydrolyzate (data not shown). The decreased viability and fermentative capacity of the yeast was likely due to ceased growth and inhibitory effects . The yeast cells were assumed to be particularly sensitive to exposure to inhibitors during the prefermentation of xylose-rich hydrolyzate liquor, because the conversion of xylose does not support growth efficiently .
Summary of results after prefermentation of hydrolyzate liquor followed by fed-batch cofermentation of enzymatic hydrolyzate
Residual sugars and end-products
S, B, 2
S, FB, 2
M, B, 1
M, FB, 1
M, B, 2
M, B, 2 c
M, FB, 2
Effect of prefermentation on overall xylitol production
Strategies employing fed-batch prefermentations elicited lower xylitol yields than those with batch prefermentation (Table 3). The xylitol production was decreased with fed-batch prefermentation, regardless of whether mild or severe slurry was used, and effected lower overall xylitol yields at the end of the fed-batch cofermentation of enzymatic hydrolyzate (Table 3). Because of the sequential targeting of xylose and glucose conversion in the fermentation steps, the xylitol productions during prefermentation were major determinants of total xylitol production. After prefermentation little xylitol was produced, because glucose was the predominant substrate and remaining xylose was mainly coconsumed.
For all practical purposes xylitol production represents a loss of carbon that could be converted to ethanol. The lower xylitol production in strategies employing fed-batch prefermentation contributed to the xylose conversion efficiency and, thus, the higher overall ethanol yields obtained. Despite lower xylose utilization the overall ethanol yields were higher than for strategies employing batch prefermentation (Table 3). The higher overall ethanol yields were correlated with the decreased xylitol production obtained with fed-batch prefermentation.
Effect of number of additions of enzymatic hydrolyzate
The multiple additions of enzymatic hydrolyzate during the fed-batch cofermentation provided the means to lower glucose concentrations in the fermentation broth, as compared to a single addition. Fed-batch SHCF of steam-pretreated wheat straw has previously been shown to enhance xylose utilization [22, 23]. However, regardless of chosen prefermentation configuration a single addition of enzymatic hydrolyzate elicited higher xylose utilization and ethanol yields than corresponding fed-batch cofermentations with two additions (Table 3). The yeast exhibited decreased xylose fermenting capacity with repetitive addition of mild enzymatic hydrolyzate that contained inhibitors. The trend was evidenced by higher final residual xylose concentrations (Table 3).
Because xylose is converted at lower rates than glucose , the fermentation time becomes of essence. The distributed multiple additions of enzymatic hydrolyzate effectively reduce the average time available for conversion of xylose that resides in the enzymatic hydrolyzate. Another aspect relates to the addition of inhibitors. The measured inhibitors were predominantly present in the separated hydrolyzate liquors, and were to a large extent converted to less toxic entities during the prefermentation. However, contributions of inhibitors were made with every addition of enzymatic hydrolyzate, because 20–30 wt % of the total amount of hydrolyzate liquor in the slurry after pretreatment remain with the solids after the filtration. In the experiment series with mild slurry the yeast was able to convert furfural irrespective of prefermentation mode and number of additions of enzymatic hydrolyzate. HMF, on the other hand, was only fully converted with batch prefermentation and one addition of enzymatic hydrolyzate (data not shown). Fed-batch prefermentation decreased the conversion of HMF, and in combination with two additions of enzymatic hydrolyzate no HMF was converted after prefermentation (data not shown). The trend in furaldehyde conversion was correlated to that of the xylose fermenting capacity. The aggregated effect of fed-batch prefermentation and multiple additions of enzymatic hydrolysate elicited increasingly higher residual xylose concentrations (Table 3), and thus lower xylose utilization. This finding was indicative of that decreases in viability of the yeast occurred with both continuous and repetitive addition of substrate that contained inhibitors.
Maximization of ethanol yield
The highest overall ethanol yield was obtained with low concentrations of inhibitor in the slurry, because it permitted feeding schemes that maximized xylose conversion efficacy while the viability of the fermenting microorganism was sustained. The best results were obtained with fed-batch prefermentation and a single addition of enzymatic hydrolyzate, with an overall ethanol yield of 0.423 g·g−1, xylose utilization of 98 %, and the lowest xylitol production at 0.036 g·g−1. The deviations from the means were below 4 % in all instances. The strategy combined lower xylitol productions and higher ethanol yields elicited by fed-batch prefermentation with the lower effect of inhibitors associated with one addition of enzymatic hydrolyzate. A trade-off existed between promoting efficient xylose conversion with substrate feeding and maintaining yeast viability. Ethanol yield was maximized with a balance between them.
The reduction in residual xylose concentrations and decreased xylitol production (Table 3), compared to the model fermentations, indicate that the sequential targeting of xylose and glucose conversion is a feasible way to improve xylose conversion with SHCF-based conversion strategies. The proposed strategy leaves degrees of freedom in the design to implement feeding schemes that accommodate the traits of various fermenting microorganisms, as to mitigate the inhibitory effects, sustain yeast viability and maximize xylose conversion.
The dilution of the retained solids after filtration of the mild slurry with the lower WIS content (11.1 wt %) was severely constrained by the required WIS load of 10 wt % in the SHCF. Hence, the retained solids were only diluted to a WIS load of 32 wt % in the enzymatic hydrolysis step. The enzymatic hydrolysis resulted in inferior hydrolysis because of various reasons associated with high WIS applications [35–37]. With inferior hydrolysis the lignocellulosic solids that remained in the enzymatic hydrolyzate were partially hydrolyzed and fermented simultaneously during the fed-batch cofermentation and the benefits of the preparatory hydrolysis of the unwashed solids waned. The simultaneous hydrolysis and cofermentation was undesirable in the SHCF, because the solids were partially hydrolyzed under suboptimal conditions at 30 °C during the fed-batch cofermentation. The drawback was not necessarily a lower yield given sufficient time, but that hydrolysis rate became a limiting factor for the fermentation rate. This constrained the final ethanol yield for the limited cofermentation period. An increase in temperature during the fed-batch cofermentation of the enzymatic hydrolyzate would have been needed to accommodate hydrolysis of remaining solids and avoid severe limitations to the fermentation rate. The illustrated limitation puts emphasis on the necessity of high sugar yields in preparatory enzymatic hydrolysis to implement the sequential targeting of xylose and glucose conversion with this strategy.
Prefermentation of hydrolyzate liquor followed by fed-batch separate hydrolysis and cofermentation improved ethanol yields, yet batch and fed-batch prefermentation had different impacts on the cofermentation. Under influence of lower inhibitor concentrations fed-batch prefermentation resulted in lower xylitol production during all steps of the fermentation and prompted higher final ethanol yields compared to corresponding cofermentations with batch prefermentation. Under influence of high inhibitor concentrations, sustained fermentation capacity was paramount to obtain improved ethanol yield. S. cerevisiae KE6-12 was resilient to high inhibitor concentrations, but succumbed to continuous exposure to inhibitors. Regardless of type of slurry, continuous feed during prefermentation of the hydrolyzate liquor and multiple additions of enzymatic hydrolyzate—and their combination—appeared to hamper the fermentative capacity and exhaust the cells. The viability of the yeast, not glucose repression of xylose metabolism, appeared to be the limiting factor for higher ethanol yields in the cofermentations. The best results were obtained with mild slurry, applying fed-batch prefermentation and a single addition of enzymatic hydrolyzate. An ethanol yield of 0.423 g·g−1, based on supplied glucose and xylose, and the lowest xylitol production, 0.036 g·g−1, was obtained. A trade-off existed between promoting xylose conversion with substrate feeding and maintaining yeast viability, and ethanol yield was maximized with a balance between them.
filter paper unit
high-performance liquid chromatography
separate hydrolysis and cofermentation
simultaneous saccharification and cofermentation
gas volume flow per unit of liquid volume per minute
FN participated in the conception and design of the study, performed the experiments and wrote the manuscript. GZ participated in the conception and design of the study and critically reviewed the manuscript. OW and MG assisted in interpreting the data, participated in the editing and preparation of the final manuscript, and critically reviewed the manuscript. All authors read and approved the final manuscript.
The Swedish Energy Agency is gratefully acknowledged for their financial support (Process development for combined pentose and hexose fermentation, 35354-1), as is Taurus Energy AB for cofinancing the project.
The study was part of the project “Process development for combined pentose and hexose fermentation”, which was co-financed by Taurus Energy AB. GZ is a shareholder and member of the board at Taurus Energy AB. Remaining authors declares no financial competing interests and all authors declare that they have no non-financial competing interests.
Open AccessThis article is distributed under the terms of the Creative Commons Attribution 4.0 International License (http://creativecommons.org/licenses/by/4.0/), which permits unrestricted use, distribution, and reproduction in any medium, provided you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons license, and indicate if changes were made. The Creative Commons Public Domain Dedication waiver (http://creativecommons.org/publicdomain/zero/1.0/) applies to the data made available in this article, unless otherwise stated.
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