Quantitative evaluation of yeast's requirement for glycerol formation in very high ethanol performance fed-batch process
© Pagliardini et al; licensee BioMed Central Ltd. 2010
Received: 17 December 2009
Accepted: 21 May 2010
Published: 21 May 2010
Glycerol is the major by-product accounting for up to 5% of the carbon in Saccharomyces cerevisiae ethanolic fermentation. Decreasing glycerol formation may redirect part of the carbon toward ethanol production. However, abolishment of glycerol formation strongly affects yeast's robustness towards different types of stress occurring in an industrial process. In order to assess whether glycerol production can be reduced to a certain extent without jeopardising growth and stress tolerance, the yeast's capacity to synthesize glycerol was adjusted by fine-tuning the activity of the rate-controlling enzyme glycerol 3-phosphate dehydrogenase (GPDH). Two engineered strains whose specific GPDH activity was significantly reduced by two different degrees were comprehensively characterized in a previously developed Very High Ethanol Performance (VHEP) fed-batch process.
The prototrophic strain CEN.PK113-7D was chosen for decreasing glycerol formation capacity. The fine-tuned reduction of specific GPDH activity was achieved by replacing the native GPD1 promoter in the yeast genome by previously generated well-characterized TEF promoter mutant versions in a gpd2 Δ background. Two TEF promoter mutant versions were selected for this study, resulting in a residual GPDH activity of 55 and 6%, respectively. The corresponding strains were referred to here as TEFmut7 and TEFmut2. The genetic modifications were accompanied to a strong reduction in glycerol yield on glucose; the level of reduction compared to the wild-type was 61% in TEFmut7 and 88% in TEFmut2. The overall ethanol production yield on glucose was improved from 0.43 g g-1 in the wild type to 0.44 g g-1 measured in TEFmut7 and 0.45 g g-1 in TEFmut2. Although maximal growth rate in the engineered strains was reduced by 20 and 30%, for TEFmut7 and TEFmut2 respectively, strains' ethanol stress robustness was hardly affected; i.e. values for final ethanol concentration (117 ± 4 g L-1), growth-inhibiting ethanol concentration (87 ± 3 g L-1) and volumetric ethanol productivity (2.1 ± 0.15 g l-1 h-1) measured in wild-type remained virtually unchanged in the engineered strains.
This work demonstrates the power of fine-tuned pathway engineering, particularly when a compromise has to be found between high product yield on one hand and acceptable growth, productivity and stress resistance on the other hand. Under the conditions used in this study (VHEP fed-batch), the two strains with "fine-tuned" GPD1 expression in a gpd2 Δ background showed slightly better ethanol yield improvement than previously achieved with the single deletion strains gpd1 Δ or gpd2 Δ. Although glycerol reduction is known to be even higher in a gpd1 Δ gpd2 Δ double deletion strain, our strains could much better cope with process stress as reflected by better growth and viability.
Ideally, a micro-organism engineered for industrial biotechnology shows high product yield, final product concentration and productivity and can cope with process constraints. Achieving all these goals is a major challenge, particularly when it comes to modifications of the central carbon metabolism which is inherently coupled to energy and redox issues. Moreover, the cell's ability to cope with environmental stress can be severely affected. One prominent example for such a challenge is the reduction of glycerol formation in Saccharomyces cerevisiae (S. cerevisiae) in order to improve yield in ethanol production. Glycerol is produced from the glycolytic intermediate dihydroxyacetone phosphate (DHAP) which is reduced to glycerol-3-phosphate (G3P) by the two homologous isoenzymes of glycerol 3-phosphate dehydrogenase (GPDH), Gpd1 and Gpd2 [1, 2]. G3P is then dephosphorylated into glycerol by the glycerol 3-phosphatases Gpp1 and Gpp2 [2, 3]. In fact, glycerol is the main by-product beside carbon dioxide and biomass, accounting for up to 5% of the carbon .
A strain showing a reduced glycerol yield to the benefit of ethanol yield would result in substantial profit for the bioethanol industry. The challenge in reducing glycerol is that this compound and its formation fulfil major physiological functions in S. cerevisiae. Glycerol formation indeed participates in maintaining cytosolic redox balance [5–8] and in providing the intermediate G3P, essential for the biosynthesis of glycerophospholipids and triacylglycerols . Glycerol is known to also contribute to stress management such as osmotic stress[10–12], heat, freezing/thawing or oxidative stress [10, 13].
Although glycerol formation by wild-type S. cerevisiae is, to a certain extent, strain dependent, it predominantly depends on the environmental conditions. The most important environmental factors are oxygen availability, type of nitrogen source, osmotic pressure, heat and pH. For example, the presence of amino acids in the growth medium reduces the requirement of producing their carbon backbones. This results in a significantly lower generation of excess NADH, i.e. lower glycerol formation when compared to minimal medium without any amino acids .
The first studies which aimed at redirecting the carbon flux toward ethanol by reducing glycerol synthesis focused on GPDH (see above). Mutants deleted in one or both isogenes encoding for GPDH were constructed in different strain backgrounds and tested for ethanolic fermentation [1, 3, 7, 14–17]. Nissen et al  reported that single deletion mutants gpd1 Δ and gpd2 Δ showed respectively a 2.8% and a 4.7% ethanol yield improvement under anaerobic conditions and a 2.2% and 3.3% under aerobic conditions. The double deletion mutant was not able to grow under anaerobic conditions and showed a 12.7% yield improvement, but also a 29% reduction in biomass yield in aerobic conditions. Other metabolic engineering strategies have targeted redox metabolism with the goal to produce less net excess NADH during the biomass synthesis and organic acid formation . Bro et al.  obtained a 3% increase in the ethanol yield without any reduction in growth rate by by-passing the NAD+-dependent glycolytic conversion of glyceraldehyde to glycerate through the heterologous expression of a NADP+-dependent glyceraldehyde-3-phosphate dehydrogenase. Nevertheless, these studies were made on low glucose concentration and did not imply industrially relevant process stresses such as high glucose and ethanol concentration. It was indeed shown that a gpd1 Δ gpd2 Δ double deletion mutant was severely affected in ethanol production (35% decrease in final titre) and ethanol tolerance (25% reduction in the Pcritical/μ value (ethanol concentration at which growth stopped)) when placed under intensive ethanol production process.
Recent studies have combined single deletion of GPD1 or GPD2, engineering of redox metabolism and/or modification of yeast glycerol export [21–25] The best results, a 39.7% reduction in glycerol yield accompanied by a 12.3% ethanol yield improvement , were obtained with a strain deleted for GPD1, FPS1 and engineered for ammonium assimilation. Though, these results were obtained in a rich medium containing amino acids which is irrelevant in regards of most industrial processes. In addition, the use of rich medium compromises a correct conclusion about the redirection of carbon flow within these strains as long as catabolism of amino acids (in addition to glucose) is not taken into account.
Although some of the studies mentioned above gave interesting results, they suffer from a lack of information in terms of fermentative capacity in a high ethanol production process in which coping with process stress such as high ethanol titers becomes a critical issue for the yeast. For this purpose we previously developed a Very High Ethanol Performance fed-batch process  as a tool for studying the yeast physiology during ethanol production processes with high productivity and final ethanol concentration. We also showed that it was possible to reduce glycerol yield and final titer by finely monitoring the Respiratory Quotient (RQ) through glucose feeding in VHEP fed-batch . However, this did not result in an increase in ethanol yield on glucose. We therefore searched for an avenue to further reduce glycerol formation in the VHEP fed-batch process. We envisaged identifying the optimal combination of process parameters and yeast strain genetic background for our process. However, it was clear from published data, that completely abolishing glycerol formation was accompanied by a drastic loss of process robustness [16, 20]. We therefore envisaged an approach where glycerol formation capacity was strongly reduced but higher than in the gpd1 Δ gpd2 Δ double deletion strain. In this context, recent advances in yeast promoter engineering [28, 29] have opened new possibilities for fine-tuning of metabolic fluxes. Based on the knowledge about Gpd1 and Gpd2 activities in yeast and available promoters for fine-tuning gene expression, an appropriate engineering strategy was defined supported by metabolic flux calculations (see results). To engineer the according strains, GPD2 was deleted and GPD1 expression was reduced by replacing its native promoter by two previously constructed TEF1 promoter versions  with strongly reduced but different activities. We present here the kinetic analysis of the two genetically modified strains by characterizing (i) the effect of the genetic modification on product formation and growth (rates, yields and titers) and (ii) the robustness of the strains in our VHEP fed-batch process.
Strains, media and growth conditions
Saccharomyces cerevisiae strains used in this study
Source or reference
van Dijken (2000) 
gpd2Δ::loxP-ble R -loxP GPD1pΔ::loxP-KanMX4-loxP-TEF1p mutant 7
gpd2Δ::loxP-ble R -loxP GPD1pΔ::loxP-KanMX4-loxP-TEF1p mutant 2
Engineered yeast strain construction
Genetic modifications of S. cerevisiae CEN.PK 113-7D carried out within this study comprise both the deletion of GPD2 and the replacement of native GPD1 promoter by two low-activity promoters (TEF1 promoters' versions see below). Gene deletion and promoter replacements based on homologous recombination in yeast were carried out according to the method described by Güldener et al.. Transformation of S. cerevisiae was carried out according to Gietz et al. using treatment with lithium acetate and polyethylene glycol. In order to allow expression of the antibiotic resistance genes cells directly after transformation were first incubated for at least 4 h at 30°C in YD containing 1% yeast extract and 1% glucose. Afterwards, cells were spread on YD agar plates supplemented with 7.5 μg/ml phleomycin (for GPD2 deletion) or 100 μg/ml geneticin G418 (for GPD1 deletion and integration of GPD1 promoter replacement cassettes).
Primers used for amplification the GPD2 disruption cassette and verification of its correct genomic integration
Forward primer for amplification of GPD2 deletion cassette
Reverse primer for amplification of GPD2 deletion cassette
Forward primer for verification of GPD2 deletion
Reverse primer for verification of GPD2 deletion
The GPD2 gene was deleted using the loxP-ble R -loxP cassette located on the plasmid pUG66 . The gene ble R confers resistance to phleomycin. The primers used for the amplification of the disruption cassette were P60 and P61 (Table 2). The GPD2 disruption cassette used here replaced 305 bp upstream of the GPD2 coding region and 360 bp of the GPD2 coding sequence. The correct integration of the loxP-ble R -loxP cassette was verified by diagnostic PCR using the primer pair P62/P63 (Table 2) and the following PCR conditions: 94°C for 1 min, 50°C for 1 min, and 72°C for 2 min. The PCR was performed in 30 cycles. If wild-type genomic DNA was used as a template, this diagnostic PCR resulted in a product of 855 bp in size, whereas the product obtained from positive gpd2 Δ transformants had a size of 1.5 kbp.
In order to replace the native GPD1 promoter by promoters of much lower activities, the TEF1 promoter mutant versions 2 and 7 of our previously published promoter collection for fine-tuning gene expression in yeast  were used. The promoters were located on the described CEN/ARS plasmids p416-loxP-KmR-TEFmut2-yECitrine and p416-loxP-KmR-TEFmut7-yECitrine bearing the loxP-KanMX-loxP cassette upstream of the TEF1 promoter mutant 2 and 7, respectively. Integrations of the low-strength promoters were confirmed by PCR diagnosis using primers and PCR conditions as described earlier  except the temperature for primer annealing was set to 57°C instead of 60°C. The PCR product obtained from native GPD1 promoter was 1.6 kbp, while a positive integration of the TEF1 promoter mutant 2 or 7 cassette yielded a product size of 2.6 kbp.
Measurement of specific GPDH activity
In order to determine the specific activity of glycerol 3-phosphate dehydrogenase (GPDH), yeast strains were aerobically grown in shake flask cultures using the synthetic minimal medium as described above supplemented with 2% [w/v] glucose. The GPDH activity was measured in logarithmically growing cells (i.e. when OD600 reached about 1) according to a previously described method [2, 34].
VHEP fed-batch protocol
VHEP fed-batch fermentations were carried on in 5 L bioreactors B DCU B.BRAUN (SARTORIUS) with a starting volume of 3 L. Temperature was set at 30°C and pH regulated at 4 by adding 14% (vol/vol) NH3 solution. The reactor was flushed continuously with air; dissolved O2 was maintained above 20% of saturation by adapting the air flow and stirring rate in order to maintain fully aerated conditions. A sequential vitamin feeding strategy based on the growth profile  was applied. The fermentations were started with an initial glucose concentration of 100 g L-1. Whenever the residual glucose concentration was lower than 20 g L-1, glucose feeding was carried out with a 700 g L-1 glucose solution to restore a glucose concentration of 100 g L-1. At the later phase of fermentation, i.e.when the ethanol concentration was above 90 g L-1, the glucose feeding adjusted the concentration to 50 g L-1.
Outlet and inlet gas analysis was performed using a mass spectrometer Proline Dycor2a (Ametek Process Instrument). Gas analysis was performed on the outlet flow of the reactor every 5 minutes and on the inlet air every hour. The volumetric O2 consumption rate and the CO2 production rate were calculated from the differences between the inlet and outlet gas compositions, taking into account the evolution of the liquid volume in the reactor, the inlet airflow rate (regulated by a mass flowmeter), the temperature and the pressure.
Yeast growth was evaluated by spectrophotometric measurements at 620 nm in a spectrophotometer Libra S4 (Biochrom) and calibrated against cell dry weight measurements. Cells were harvested by filtration on 0.45-μm-pore-size polyamide membranes (Sartorius Biolab Product) and dried to a constant weight at 60°C under a partial vacuum (200 mm Hg ~ 26.7 kPa) for 24 hours. Rapid determination of glucose and ethanol concentrations from broth supernatants during fermentation was performed with an YSI analyser (YSI model 27 A; Yellow Springs Instruments).
Determination of ethanol, organic acids and glucose from supernatants was performed by HPLC using an Aminex HPX-87H+ column (300 mm × 7.8 mm) and dual detection (refractometer and UV at 210 nm) at 50°C with 5 mM H2SO4 as an eluant (flow rate of 0.5 mL min-1). Three independent metabolite quantifications (taking into account sampling, separation and HPLC quantification) showed that the measurement was reproducible; typically standard deviation was lower than 1% of mean value for ethanol and glucose and lower than 5% for glycerol and acetate.
All chemicals were of the highest analytical grade available.
Determination of the cells' viability
To determine cells' viability, the methylene blue technique was used as previously described .
Assessment of ethanol evaporation
When balancing aerobic ethanolic fermentation experiments, there is commonly a lack in carbon due to evaporation of ethanol. In fact, this may account for more than 20% of the total carbon [16, 35]. To assess the part of evaporated ethanol, evaporation experiments were carried out under the same cultivation conditions as performed in this study but without yeast. The bioreactor was filled with 3 liters of the synthetic mineral medium used in this study and ethanol was added up to a concentration of 150 g L-1. Decrease in the ethanol concentration was recorded over time by taking regular liquid samples and HPLC quantification. The rate of evaporation was found to be dependent on ethanol concentration, aeration rate and liquid volume. No significant impact of stirring on evaporation was observed which is in accordance to a previous study . Evaporation was investigated for the 2 aeration rates used during the fermentations 1 L.mn-1 and 0.5 L.mn-1. Based on these data, an evaporation rate was attributed to each ethanol liquid concentration. Integration of this evaporation rate over time and liquid volume allowed calculating the evaporated ethanol in our yeast fermentations. The fact that the measured ethanol evaporation during the period of fermentation when cells had stopped producing ethanol exactly matched the calculated ethanol evaporation validated the method.
Metabolic Flux Calculation
Metabolic fluxes were calculated using a MFA based model extrapolated from a previously described Metabolic Descriptor [27, 36] The metabolic network was modified by adding mitochondrial compartmentation. Repartition of the reactions between cytosol and mitochondria was made according literature and previously described models [37–42]. Glycolysis, pentose phosphate pathway, synthesis of amino-acid precursors and nitrogen bases as well as formation of ethanol and glycerol were attributed to the cytosol. TCA cycle and respiratory chain were attributed to the mitochondria. Acetate and acetyl-coA synthesis were assumed to be localized in both cytosol and mitochondria. Segregation of amino acids synthesis between cytosol and mitochondria was inserted into the model according to the literature cited above. All transport reactions between the cytosol and the mitochondria were assumed to be simple transport reactions except for redox equivalent translocation via the glycerol shuttle. Our final metabolic network consists in 142 reactions, including 14 exchange reactions between the cell and external medium, 88 cytosolic reactions, 24 transport reactions between mitochondria and cytosol, and 16 mitochondrial reactions (cf. Additional file 1). Validity of the model was assessed using published data based on 13C labelling experiments [43, 44].
OP: Oxidative Phosphorylation
TCA: Tricarboxylic acid cycle
NADHcon: NADH consumed
NADHpro: NADH produced
The uncertainties of the TCA cycle fluxes values were estimated to impact the Yatp,x and NADH balance by less than 3%.
Design and construction of the GPD engineered strains supported by in silico flux calculations
In order to engineer S. cerevisiae strains with a strongly reduced but not completely abolished glycerol formation capacity, we envisaged to delete one isogene of GPDH and fine-tune the expression of the other one by replacing its native promoter by another one with much lower activity. We decided to delete GPD2 and fine-tune GPD1 expression since the latter is known to be responsible for the major part of GPDH activity and GPD2 deletion has been demonstrated to have no major impact on yeast physiology except when synthetic minimal medium was used under strictly anaerobic conditions . In order to replace the native GPD1 promoter in CEN.PK 113-7D gpd2 Δ background, two previously characterized mutated versions of the S. cerevisiae TEF1 were used (see Material and Methods). We chose the two weakest promoters available for this study, i.e. TEF1 p mutant 2 (normalized promoter strength 7%) and TEF1 p mutant 7 (promoter strength 16% normalized to the native TEF promoter) . Specific GPDH activity of the wild type was 0.041 U/mg protein. The down-regulation of GPD1 gene expression by GPD1 promoter replacement in the gpd2 Δ background resulted in significantly reduced GPDH activities. The use of TEF1 p mutant 7 upstream of GPD1 reduced GPDH activity to 55% (0.023 U/mg protein) whereas the use of TEF1 p mutant 2 reduced GPDH activity to 6% (0.006 U/mg protein) compared to wild-type activity.
Impact of reduced GPDH activity on fermentations parameters
Fermentation characteristics for S. cerevisiae wild-type strain CEN.PK 113-7D and the two mutants
Fermentation Time (h)
Growth Time (h)
Final Volume (L)
μ max (h -1 )
0.35 ± 0.02
0.28 ± 0.02
0.24 ± 0.02
DCWmax (g L -1 )
15.7 ± 0.5
14.5 ± 0.5
14.5 ± 0.5
YDCW/glucose g g -1
0.093 ± 0.006 [5-15 h]
0.091 ± 0.007 [5-15 h]
0.087 ± 0.005 [5-17 h]
Yethanol/glucose g g -1 (growth)
0.41 ± 0.006 [0-20 h]
0.42 ± 0.01 [0-20 h]
0.44 ± 0.005 [0-23 h]
Yethanol/glucose g g -1 (overall)
0.43 ± 0.005 [0-55 h]
0.44 ± 0.008 [0-49 h]
0.45 ± 0.003 [0-49 h]
Y glycerol/glucose mg g -1
13 ± 0.01 [0-20 h]
5.1 ± 0.2 [0-20 h]
1.6 ± 0.1 [0-23 h]
[ethanol] final (g L -1 )
112 ± 4
114 ± 4
[glycerol] final (g L -1 )
3.1 ± 0.1
1 ± 0.1
0.4 ± 0.1
Ethanol Productivity (g L -1 h -1 )
2.13 ± 0.15
2.2 ± 0.15
2.3 ± 0.15
Pcritical/μ (g L -1 )
87 ± 3
85 ± 3
86 ± 3
The final biomass concentration obtained for the wild-type strain was 15.7 g L-1 while both modified strains showed a final biomass concentration of 14.5 g L-1. Final glycerol concentration was 3.1 g L-1 for the wild-type strain compared to 1 g L-1 for TEFmut7 and 0.4 g L-1 for TEFmut2. The final ethanol concentration reached was 117 g L-1 for the wild-type and slightly reduced to 112 g L-1 for TEFmut7 and 114 g L-1 for TEFmut2. At the end of fermentation, acetate concentration reached 5.5 g L-1 in the wild type and 5.1 g L-1 in the two mutants.
Impact of reduced GPDH activity on fermentation kinetic parameters
The reduction of GPDH activity in the engineered strains led to a decrease in the maximum specific glycerol production rate from 0.083 g gDCW h-1 in the wild type to 0.023 g gDCW h-1 and 0.004 g gDCW h-1 in TEFmut7 and TEFmut2, respectively. This corresponds to 28 and 5% residual rates in TEFmut7 and TEFmut2 compared to the wild type, respectively. However, the maximum specific growth rate and the maximum specific ethanol production rates were also reduced in the strains engineered for lower GPDH activity. The μmax was 0.35 h-1 for the wild type, 0.28 h-1 for TEFmut7 and 0.24 h-1 for TEFmut2. The maximum specific ethanol production rates were 1.31 gethanol gDCW-1 h-1 in the wild type, 1.10 gethanol gDCW-1 h-1 in TEFmut7 and 0.98 gethanol gDCW-1 h-1 in TEFmut2 corresponding to 16% and 25% reduction in the strains TEFmut7 and TEFmut2, respectively. Nevertheless, the overall volumetric ethanol productivity was hardly affected in TEFmut7 and TEFmut2, i.e. 2.2 ± 0.1 and 2.3 ± 0.1 g L-1h-1, respectively compared to 2.1 ± 0.15 g L-1h-1 for the wild type.
Impact of reduced GPDH activity on yields
Glycerol yield based on consumed glucose was 0.0051 g g-1 and 0.0016 g g-1 for TEFmut7 and TEFmut2, respectively, corresponding to 39% in TEFmut7 and 12% in TEFmut2 compared to the wild type strain (0.013 g g-1). The glycerol yields per g of biomass during the growth phase were also much lower for TEFmut7 and TEFmut2 (i.e. 0.06 and 0.02 g g-1DCW) respectively, compared to 0.14 g g-1DCW for the wild type.
The biomass yields on glucose in TEFmut7 and TEFmut2 were slightly lower in the strains with the reduced GPDH activity, i.e. 0.091 gDCW gglucose-1 for TEFmut7 and 0.087 gDCW gglucose-1TEFmut2 compared to 0.093 gDCW gglucose-1 for the wild type. The overall acetate yields based on consumed glucose were similar for all three strains and reached 0.017 g g-1.
As a result, the overall ethanol production yield on glucose was increased in the two engineered strains. While the wild-type strain produced 0.43 g g-1, TEFmut7 formed 0.44 g g-1 and TEFmut2 0.45 g g-1. As visible from Table 3, the strain differences in the overall ethanol yields were solely due to the differences observed during the growth phase. In this phase, ethanol yields reached 0.41 g g-1 for the wild type, 0.42 g g-1 for TEFmut7 and 0.44 g g-1 for TEFmut2. During the "production phase", no significant variation of ethanol yield could be observed between the wild type and the two engineered strains (0.47 g g-1).
We also calculated oxygen to biomass yield for all three strains. The average oxygen to biomass yield during the growth phase of the wild type was 6 mmolO2 gDCW-1. While there was no significant difference compared to TEFmut7 (7 mmolO2 gDCW-1), the strain TEFmut2 showed a significantly higher yield of 10 mmolO2 gDCW-1.
Impact of reduced GPDH activity on ethanol tolerance
Comparative flux analysis of the strains
Aiming at determining to what extent glycerol formation may be reduced without affecting drastically the strain robustness in a VHEP fed-batch process, the modulation of glycerol synthesis capacity of S. cerevisiae was obtained by replacing the native promoter of GPD1 with promoters of significantly lower activities in a CEN.PK113-7D gpd2 Δ background resulting in the strains TEFmut7 and TEFmut2.
Fine-tuning of the glycerol synthesis pathway led to improved ethanol yield
The two engineered strains led to a reduction of glycerol yield on glucose by 61% for TEFmut7 and 88% in TEFmut2 compared to the wild type strain. The metabolic flux calculation from the experimental data set of TEFmut7 and TEFmut2, respectively, showed that the DHAP-to-G3P flux was evaluated at 39 and 11% of the one calculated in the wild type (Figure 5). The reduction of the glycerol production in the two engineered strains was accompanied by a slightly increased ethanol yield on glucose (2.3% for TEFmut7 and 4.6% for TEFmut2). For comparison, in aerobic conditions, simple deletion mutants gpd1 Δ and gpd2 Δ of TN1 strain showed respectively a 2.2% and 3.3% yield improvement, whereas double deletion gpd1 Δgpd2 Δ strain showed a 12% improvement (0.39 g g-1) . A 10% ethanol yield improvement was also obtained in a double deletion gpd1 Δ gpd2 Δ strain of W303-1A but was accompanied by a drastic loss of robustness towards ethanol stress .
Fine-tuning of the glycerol synthesis pathway altered the growth rate but not the ethanol tolerance in VHEP
The mitochondrial shuttles were represented in the model by the glycerol-3-phosphate shuttle, but either an increased participation of the external NADH dehydrogenases (NDE1/2) or the glycerol-3-phosphate shuttle could take over the excess of cytosolic NADH [8, 48]. Therefore both systems likely participated to the transfer of cytosolic NADH into the mitochondria to be oxidised by the respiratory chain leading to the increase in the O2 consumption. However the reduction of the GPDH rate may have reduced the activity of the glycerol-3-phosphate shuttle compared to the NDEs in our engineered strains. As the glycerol-3-phosphate shuttle was reported to have a higher ATP/O ratio compared to the external NDEs, the reduction of the glycerol-3-phosphate shuttle activity could partly explain the reduction in Yx,ATP in our mutant strains .
One alternate explanation for growth rate reduction might be that the reduction in the glycerol phosphate dehydrogenase rate created a competition for the L-G3P between the anabolic requirement in this metabolite and glycerol synthesis within the cell. L-G3P produced by the reduction of DHAP is indeed either dephosphorylated into glycerol by the glycerol phosphate phosphatases (GPP) or enters into the phospholipid synthesis pathway via the phosphatidic acid (Figure 1). The rate of dephosphorylation of L-G3P being far higher than the rate of its conversion into phosphatidic acid, this latter reaction might limit the growth rate.
No relevant reduction of the maximum specific growth rate was observed in single gpd Δ deletion mutants in previous studies in aerobic conditions . However ethanol production capacities of these strains were studied under experimental conditions where the cells did not face high glucose and high ethanol concentration as encountered in VHEP conditions. Glycerol is known to play a role in stress resistance, such as osmotic stress [10, 49], ethanol and temperature stress . Glycerol is the major compatible solute accumulated in yeast to increase cell turgor pressure to face hyper-osmotic stress. Modifying the glycerol synthesis pathway should alter the ability of the cell to regulate its turgor pressure. However authors have suggested through the surface stress theory that a fine tuned turgor pressure is necessary for yeast growth [50, 51]. Thus an impact of the osmotic stress on the μmax of our strains under our conditions cannot be completely excluded.
Despite the impact on the growth rate and in clear contrast to the gpd1 Δgpd2 Δ double deletion strain , ethanol tolerance was not affected by the genetic modifications carried out in the current study even though the fermentation conditions were exactly the same.
Finally we concluded that the two mutant strains were able to sustain a similar ethanol concentration than the wild type strain but with a higher energy expense. This higher energy demand increased the relative weight of energy production reactions over biomass synthesis in the metabolism of the mutants leading to an improved ethanol yield.
A prominent feature here is that fine-tuning the glycerol synthesis pathway (within the range 11-39% of the wild-type capacity) allows the strains to keep their initial ethanol tolerance. Both engineered strains showed indeed a similar behaviour in terms of ethanol inhibition on growth quantified by a Pcritical/μ value at 86 ± 1 g L-1 and viability. Therefore we conclude that reducing the glycerol synthesis down to 11% of the wild type capacity did not affect the strain robustness in terms of ethanol tolerance, ethanol titer and productivity.
This work was supported by grants from the P2R Program (French Ministry of Foreign Affairs, CNRS and DAAD) and from the ANR program (ANR-05-BIOE-007). J. Pagliardini gratefully acknowledges financial doctoral support by the ADEME and Danisco France.
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