Impact of oleic acid as co-substrate of glucose on “short” and “long-term” Crabtree effect in Saccharomyces cerevisiae
© Marc et al.; licensee BioMed Central Ltd. 2013
Received: 19 July 2013
Accepted: 4 September 2013
Published: 23 September 2013
Optimization of industrial biomass directed processes requires the highest biomass yield as possible. Yet, some useful yeasts like Saccharomyces cerevisiae are subject to the Crabtree effect under glucose excess. This phenomenon can occur in large scale tank where heterogeneities in glucose concentrations exist. Therefore yeasts encounter local environments with glucose excess leading to ethanol production to the detriment of biomass formation. We previously demonstrated that oleic acid as a co-substrate in glucose-limited chemostat allowed to delay and modulate the “short-term” Crabtree effect in Saccharomyces cerevisiae. Here we further investigated the effect of oleic acid as a modulator of the Crabtree effect.
The impact of oleic acid as co-substrate on the Crabtree effect was investigated in terms of i) strain specificity, ii) reversibility of the potential effect with aerobic glucose-excess batches and iii) durability and maximal capacities under high ethanol stress with glucose-excess fed-batches. First, the addition of oleic acid resulted in an increase of the critical dilution rate by 8% and the specific carbon uptake rate by 18%. Furthermore, a delay was observed for the onset of ethanol production when a batch was inoculated with cells previously grown in glucose-oleate chemostat. Finally, the culture of adapted cells in a glucose-oleate fed-batch led to a redirection of the carbon flux toward biomass production, with a 73% increase in the biomass yield.
This work demonstrated clearly that the perturbation by oleic acid as co-substrate resulted in a decrease in the “short-term” and “long-term” Crabtree effects. This impact was not strain dependent and reversible. Thus, industrial applications of this biochemical strategy could be envisaged to tackle heterogeneities issues in large scale tanks or to prepare starter yeasts for various applications.
KeywordsSaccharomyces cerevisiae Ethanolic fermentation Oleic acid Crabtree effect Accelerostat Batch Fed-batch
The repression of oxidative pathways by glycolytic activity resulting in simultaneous fermentation and respiration was named “Crabtree effect” [1–3]. The resulting oxido-reductive metabolism is characterized by a byproduct formation (ethanol, glycerol and weak acids), a loss in biomass yield and a limited oxygen specific uptake rate. It is named “long-term” effect when it appears in glucose excess batch and fed-batch or in glucose-limited chemostat at dilution rates over the critical dilution rate (Dc), involving adaptation of cell metabolism, while it is named “short-term” effect after a glucose pulse in glucose-limited chemostat at dilution rates under Dc.
The mostly global accepted theory to explain this mechanism is a limited respiratory capacity in Crabtree-positive cells. This respiratory capacity includes the whole cytosolic and mitochondrial pathways responsible for the respiratory catabolism of pyruvate, including the respiratory chain. It is saturated above a critical threshold of glucose uptake rate. Then, the cell directs the excess of glycolytic flux toward fermentative metabolism with apparition of ethanol production [5, 6]. This theory was supported by studies using genetic engineering approach. However, isolated deletion or over-expression of various genes coding for enzymes within the respiratory capacity did not success to bring out any single limiting reaction [7–15].
Modulation of the metabolic transition was successfully reported after engineering global regulation functions. The deletion of MIG1 and MIG2, coding for a positive regulator in glucose repression led to a 5% higher Dc, at 0.274 h-1. The over-expression of HAP4, coding for a positive regulator of genes involved in respiratory metabolism, led to a 10% higher Dc, at 0.33 h-1. Decreasing intracellular NADH/NAD+ ratio by expressing a heterologous gene coding for a mitochondrial oxidase (AOX1) led also to a 10% higher Dc, at 0.32 h-1. Furthermore, modulation of “short-term” Crabtree effect was also reported through co-substrate feeding. Feeding oleic acid as a co-substrate of glucose enabled to delay and modulate the “short-term” metabolic transition apparition in cells .
The latter approach was carried out by feeding an aerobic glucose-limited chemostat at D = 0.16 h-1 with oleic acid. After a glucose pulse of 10 g L-1, a delay up to 15 min in the onset of the metabolic shift, a 33% decrease in the ethanol production, and a redirection of the carbon flux toward biomass production were observed. Moreover, specific activities of carnitine-acetyl transferase, isopropylmalate synthase and citrate synthase were increased. These ones are enzymatic systems involved in the transport of acetyl-coA through the mitochondria membrane [20–24]. Nevertheless, explanation of oleate effect on the metabolism remained unclear. First, the presence of this acid as co-substrate of glucose may have induced a “substrate effect” (degradation of the oleic acid through the β-oxidation pathway introducing a supplemental carbon flux into the central metabolism with potentially allosteric modifications). Feria-Gervasio et al.  conducted a glucose pulse experiment during a glucose-succinate chemostat in order to mimic the substrate effect of the oleic acid, but data obtained suggested that the “substrate effect” was not the major effect responsible for the decrease in the transition from respiratory to fermentative metabolism. Secondly, oleic acid may have induced a “genetic effect”, acting at the transcriptional and / or translational level via regulatory complex systems. Indeed, this acid is known to induce the transcription of various genes possessing the ORE (Oleate Response Element) sequence on their promoter . This last hypothesis was strengthened by the observation of increased specific activities of enzymes coded by such genes in presence of oleic acid .
These previous efforts led to an overview of the impact of oleic acid on the “short-term” Crabtree effect. Nonetheless, the processes used for industrial applications for which Crabtree effect is unwanted, like starter yeasts or heterologous protein production, could led to “long-term” as well as “short-term” Crabtree effect. Moreover, the range of S. cerevisiae strains used in industry is wide and their behavior could largely differ from CEN.PK 113-7D. Based on these observations, previous work of Feria-Gervasio et al.  needed to be completed. Thus in the present work, we further investigated the impact of oleic acid including a determination of its specificity using an industrial strain (S. cerevisiae CA10/pCD63), the determination of the critical dilution rate for purely oxidative metabolism (Dc), an investigation of the reversibility of the effect and finally a characterization of the durability of the effect under conditions resulting in “long-term” Crabtree effect onset.
Results & discussion
We previously demonstrated that oleic acid as a co-substrate in glucose-limited chemostat (D=0.16 h-1) allowed to delay and modulate the transition from respiratory to oxido-reductive metabolism, so called “short-term” Crabtree effect, in Saccharomyces cerevisiae CEN.PK 113-7D. As a consequence of the modulation of the transition, ethanol production was decreased and the carbon flow was redirected toward the biomass production . In order to further characterize this effect, the impact of oleic acid was investigated in terms of strain specificity, durability and reversibility of the effect.
The oleic acid impact was not specific to the CEN.PK 113-7D strain
Thus, the impact of oleic acid on the dynamic profiles of ethanol production and RQ were similar for both strains, however less slightly pronounced for S. cerevisiae CA10/pCD63.
Oleic acid impacted also the critical dilution rate (Dc)
In order to determine the critical dilution rate for S. cerevisiae CEN.PK 113-7D with and without oleic acid as co-substrate (D=0.0073 h-1), accelerostat cultures were carried out by increasing the glucose feeding as a function of time. The dilution rate was increased from an initial value of 0.16 h-1 to a final value of 0.30 h-1 with a constant acceleration of 0.005 h-2.
In regard to the total carbon (glucose and oleic acid) uptake rate, the Dc corresponds to a 15% higher carbon uptake rate in glucose-oleate A-stat, from 16.5 to 19.0 mCmol gDCW-1 h-1 (Figure 3), oleic acid carbon accounting for 7%.
Oleic acid effect was at least partially reversible
Batch cultures were performed in order to determine the reversibility of the oleate impact. Pre-grown cells on glucose-oleate carbon source were transferred in glucose batch cultures with or without oleic acid as co-substrate (BGCGO and BGOCGO). Their ethanolic performances were compared to a control glucose batch with cells precultured on glucose only (BGCG).
Oleic acid impact was effective for hours during VHEP fermentation under oleate pressure
The impact of oleic acid on the oxido-reductive metabolism and its durability were further studied during fed-batch conditions. A first glucose-excess aerobic fed-batch cultivation was carried out with glucose as sole carbon source inoculated with cells precultured on glucose (FBGCG). A second fed-batch was carried out with cells pregrown on glucose and oleic acid as co-substrate (FBGOCGO) for comparison.
Final concentrations, global yields and maximal specific rates obtained during aerobic fed-batch cultivations
FB G C G
g L -1
13.2 ± 0.3
126.8 ± 0.6
4.96 ± 0.02
5.28 ± 0.04
0.53 ± 0.01
0.36 ± 0.01
FB GO C GO
g L -1
22.9 ± 0.5
116.2 ± 1.1
4.21 ± 0.05
5.1 ± 0.1
0.71 ± 0.03
0.37 ± 0.06
FB G C G
g g -1
0.174 ± 0.005
0.432 ± 0.008
0.0142 ± 0.0012
0.0158 ± 0.0006
0.0027 ± 0.0006
0.0013 ± 0.0003
FB GO C GO
g g -1
0.234 ± 0.012
0.40 ± 0.01
0.015 ± 0.002
0.0171 ± 0.0004
0.0045 ± 0.0002
0.0013 ± 0.0002
Maximal specific rate
FB G C G
g g -1 L -1
0.35 ± 0.01
1.31 ± 0.05
0.074 ± 0.008
0.034 ± 0.004
0.007 ± 0.002
0.013 ± 0.004
FB GO C GO
g g -1 L -1
0.38 ± 0.03
0.43 ± 0.03
0.045 ± 0.008
0.047 ± 0.002
0.015 ± 0.003
0.017 ± 0.004
Table 1 showed a greater production of succinate in the cells precultured on glucose + oleic acid (FBGOCGO). Final concentration, global yield and maximal specific rate of production of this organic acid were increased respectively by 34%, 67% and 114% when oleate was added in the fermentation broth. Measurements did not reveal any oleate consumption during the fed-batch FBGOCGO experiment. Moreover carbon mass balance was found close to 100% taking into account only glucose as substrate, confirming that no oleic acid was consumed. Therefore, a succinate synthesis from the catabolism of oleic acid through the β-oxidation and glyoxylate pathways cannot be taken into consideration. The cycle of the tricarboxylic acids was then supposed to be the source of succinate excretion under fermentative metabolism with glucose as sole carbon source, as previously mentioned by Camarasa et al. . Moreover, HCO3- was known to inhibit numerous enzymes such as TCA cycle succinate dehydrogenase . During our experiments, succinate was produced in the first phase of the fed-batches, corresponding to the slightly extended growth phase, corresponding when the highest rates of CO2 production occurred (results not shown). Assuming that succinic acid derived from the tricarboxylic acids cycle (TCA), the increased excretion of succinate could be interpreted as a higher activity of the TCA cycle. These observations were strengthened by the increased oxygen consumption observed in presence of oleic acid (data not shown) and previously described by Feria-Gervasio et al.  in aerobic chemostat.
Glycerol production was also decreased in presence of oleic acid. Final concentration and maximal specific rate of production of glycerol were decreased respectively by 15% and 39%. In addition to its role in the stress response, glycerol formation is known to ensure the cytosolic NADH reoxidation when oxido-reductive metabolism occurs for anabolic purpose . The decrease in glycerol production was likely the result of the increase in the oxygen consumption rate observed in the presence of oleic acid. Similar correlation between glycerol formation and oxygen consumption rate were reported in the literature either by modulating the aeration regime , by reducing the glycerol production through the control of the RQ  or by metabolic engineering approaches [18, 31].
Considering the differences on succinate, pyruvate, glycerol productions and on oxygen consumption, we can reasonably make the statement that the presence of oleic acid enhanced the global respiratory capacity in S. cerevisiae.
Implication for scale up biomass production process
The understanding and control of biomass production processes present an important interest from an economical point of view. The main microorganism used for these processes is Saccharomyces because of its utilization in a wide variety of food industries. Van hoek et al.  showed that the quality of commercial baker’s yeast (S. cerevisiae) was determined by many parameters including storage, stability, osmotolerance, freeze-thaw resistance, rehydratation resistance and color.
Nevertheless, this particularity is quite undesirable during biomass production since it reduces the biomass yield on the carbon feedstock. For this reason, industrial starter yeast production is performed in aerobic, sugar-limited fed-batch cultures. The optimization of process productivity therefore requires the higher increase as possible of the specific growth rate and / or of the biomass yield. Process optimization has been so far based on strain selection and empirical optimization of the environmental parameters such as pH, temperature, aeration rate and feeding profiles of sugar, nitrogen and phosphorus [36–38].
Moreover, large tanks used for industrial production lead to scale-up difficulties due to the appearance of heterogeneities, in particular for glucose and oxygen concentrations. Mixing time was estimated between 10 seconds and 250 seconds considering the tank size from 12 to 30 m3[39–42]. Mimicking the cell life in bioreactor was done with complex systems of bioreactors presenting different substrate and oxygen conditions. It revealed onsets of metabolic rearrangements in the order of the second [39, 43]. The present study and previous work of Feria-Gervasio et al.  showed that addition of oleic acid in the fermentation broth permitted the yeast to present a delay for the metabolic shift onset after a sudden increase of glucose concentration in the range of few minutes.
Thus, an industrial use of oleic acid in such processes could lead to better manage the heterogeneities issues when the Crabtree effect onset is not desirable. Moreover, we demonstrated that the impact of oleate was not strain dependent but reversible. Therefore, starter yeasts prepared with oleate as co-substrate of glucose could be further used in various applications, implementing the Crabtree effect or not.
In this work we demonstrated that adding oleic acid as a co-substrate of glucose allowed to decrease the occurrence of the “short-term” Crabtree effect as well as the “long-term” one. In both cases, biomass production was widely enhanced to the detriment of ethanol, and an 8% increase in the critical dilution rate has been reported. Because these biochemical phenomena were shown to be not strain dependent but reversible, industrial applications could be rationally envisaged in various purposes requiring a more efficient control of the Crabtree effect.
Strain and media
The yeast strain S. cerevisiae CEN.PK 113-7D  and CA10/pCD63 (provided by Sanofi Aventis industry) were stored in 30% glycerol at -80°C. CA10/pCD63 was auxotroph for adenine and histidine . The cells were first grown on YPD plates (10 g L-1 yeast extract, 20 g L-1 bactopeptone, 20 g L-1 glucose, 15 g L-1 agar) at 30°C. All subsequent pre-cultures and culture experiments were carried out at 30°C in mineral medium as described by Feria-Gervasio et al. , except for fed-batch technique. When using the CA10/pCD63 strain the mineral medium was supplemented with adenine and histidine in the reservoir medium at 0.2 g L-1. Medium used for fed-batch experiment contained per litre: KH2PO4, 6 g; (NH4)2SO4, 12 g; MgSO4, 1 g. A sequential vitamins and trace elements feeding strategy based on the growth profile was applied  to reach per liter: EDTA, 0.03 g; ZnSO4.7H2O, 0.009 g; MnSO4.H2O, 0.002 g; CoCl2.6H2O, 0.0006 g; CuSO4.5H2O, 0.0006 g; Na2MoSO4.2H2O, 0.008 g; CaCl2.2H2O, 0.009 g; (NH4)2Fe(SO4)6.6H2O, 0.006 g; H3BO3, 0.002 g; D-biotin, 0.00024 g; D-L-pantothenic acid, 0.005 g; nicotinic acid, 0.005 g; myo-inositol, 0.125 g; thiamin, 0.005 g; pyridoxin, 0.005 g; para-aminobenzoic acid, 0.001 g.
Chemostat cultivations with S. cerevisiaeCA10/pCD63
Chemostat cultures with glucose as the sole carbon source and with glucose plus oleate were performed as described by Feria-Gervasio et al. . The dilution rate was set at 0.18 h-1 for S. cerevisiae CA10/pCD63 to maintain the cells under pure oxidative metabolism. The bioreactors were fed with the mineral medium supplemented with glucose at 38 g L-1 for glucose chemostat and 39 g L-1 for glucose-oleate chemostat. This glucose-oleate chemostat was also fed with a 720 g L-1 oleic acid solution at a dilution rate of 0.0041 h-1.
After establishment of the steady state, six independent samples were taken over a period of 40 h to characterize it. Then glucose pulses were performed by injecting a known volume of a 600 g L-1 glucose solution in order to obtain a concentration in the reactor of 10 g L-1. The influent and effluent pumps were running continuously during the experiment. These experiments were carried out twice for each condition in two independent chemostats.
Accelerostat cultivations with S. cerevisiaeCEN.PK 113-7D
Where: Dt is the dilution rate for the instant “t”; D0 represents the initial dilution rate; α is the constant acceleration rate fixed and t the time in hours.
Batch cultivations with S. cerevisiaeCEN.PK 113-7D
Summary of the different experiments carried out in the present study
CultureC. source / CellsC. source
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
Glucose / Oleate
VHEP fed-batch cultivations with S. cerevisiaeCEN.PK 113-7D
Fed-batch cultures were performed in a 5 L bioreactor B DCU B.Braun with a working volume of 3 L, managed with the MFCS/win 2.0 software. Temperature was regulated at 30°C and pH at 4.0 by addition of 14% (v/v) NH3 solution. Air flow and stirring rate were adjusted to maintain fully aerobic condition, i.e. a dissolved oxygen concentration above 20% of saturation. Initial glucose concentration was 100 g L-1 for all experiments, supplemented with oleic acid at 50 g L-1 for the glucose-oleate fed-batch. When glucose concentration reached 20 g L-1 in the bioreactor, pulses of a 700 g L-1 glucose solution was achieved to reach 100 g L-1. At the later phase of cultivation, i.e. when ethanol concentration was above 90 g L-1, the targeted glucose fed concentration was 50 g L-1. For glucose-oleate fed-batch (FBGOCGO), oleic acid feeding strategy was also performed to maintain the 50 g L-1. Inoculation was done from YPD plate of S. cerevisiae CEN.PK 113-7D. Three steps of propagation were carried out (5 mL, 30 mL and 300 mL) to inoculate the fed-batch cultures. Each preculture was grown for 10 hours at 30°C, 100 rpm and was used to inoculate the next-step at 10% (v/v) ratio. For glucose-oleate fed-batch cultivation, cells were firstly adapted to oleic acid by a growth phase in the bioreactor on 10 g L-1 trehalose, supplemented with 50 g L-1 of oleic acid. This strategy was carried out in order to mimic oxidative chemostat culture on glucose-oleate . When trehalose was fully consumed, glucose was feed to reach 100 g L-1 and the culture was done as described above. Ethanol assessment was done as described by Pagliardini et al.  and taken into account for further calculations.
Inlet and outlet gases compositions were analyzed by mass spectrometry. For chemostats and A-stats, analyses were performed every 5 min during the steady state, every 45 s during A-stats acceleration and every 5 s during the pulse dynamic with a PRIMA 600s (VG gas, Manchester, UK). For batches and fed-batches, analyses were performed every 5 min with a Proline Dycor (Ametek Process Instrument, Berwyn, USA). Aeration started 1 hour after inoculation to avoid CO2 stripping from the medium and then prevent lag phase. CO2 production rate and O2 consumption rate were calculated as described by Poilpre et al.  for chemostats, A-stats and batches, and considering the liquid and gas volume evolution, the inlet airflow, the temperature and the pressure. The Respiratory Quotient (RQ) was given by the molar ratio between rCO2 and rO2.
Determination of biomass
In order to conduct experiments, spectrophotometric measurements at 620 nm were performed with spectrophotometers Hitachi U- 1100 (Hitachi High Technologies America Inc., Schaumburg, USA) or Libra S4 (Biochrom, Cambridge, UK) after a calibration against cell dry weight measurements to evaluate yeast growth. For cell dry weight determination, culture medium was harvested and filtrated on 0.45 μm pore-size polyamide membranes (Sartorius AG, Göttingen, Germany), which were then dried to a constant weight at 60°C under partial vacuum (200 mmHg, i.e. approximately 26.7 kPa). In presence of oleic acid, 500 μl of culture medium were mixed with 500 μl of iso-propanol to eliminate oleic acid. The mixture was vortexed for 1 min and centrifuged for 3 min at 12.000×g. The pellet was resuspended in 500 μl of water for spectrophotometric measurements. For cell dry weight determination, membranes were washed after filtration with hexane and water to eliminate oleic acid. It was previously checked that iso-propanol and hexane did not damage the cells.
Determination of cell viability
A cell coloration with the methylene blue method  was used as previously described to determine cells viability . In presence of oleate, cell suspension was prepared as described above before staining procedure.
Sampling for metabolite analysis was performed by sampling the broth from bioreactors directly through a sterile 0.45 μm pore-size polyamide membranes (Sartorius AG, Göttingen, Germany). The permeate was then either directly analyzed (chemostats and A-stats) or frozen at -20°C for further analyses (batches and fed-batches).
In order to conduct experiments, glucose concentration was analyzed by enzymatic method with an YSI analyser model 27 A (YSI Life Science, Yellow Springs, USA). The accurate determination of glucose, ethanol, glycerol and organic acids from the permeate was performed by high-performance liquid chromatography (HPLC) as described by Alfenore et al. . For chemostats and A-stats, the concentrations of ethanol and acetic acid were determined by gas chromatography as described by Feria-Gervasio et al. .
Oleic acid concentration determination was performed by two methods on the filtered supernatant obtained after iso-propanol washing and centrifugation. On the first hand, supernatant was directly injected in a HPLC using a 250*4.6 mm C18 column (Interchim, Montluçon, France). Column temperature was set at 50°C and a 3% (v/v) acetic acid in methanol solution was used as carrier with a flow rate of 1 ml min-1. Detection was done with a refractometer. On a second hand, supernatant was processed with a 0.2 mol L-1 trimethylsulphonium hydroxide in methanol solution in order to turn fatty acids into volatile molecule by methylation of their carboxilic function. Then sample was analyzed by gas chromatography using a 50 m*0.25 mm CP-Select CB for FAME fused silica WCOT (Varian, Palo Alto, USA). Injector temperature was set at 140°C and column temperature was initially set at 50°C, then be increased to 240°C with the following profile: 8°C min-1 for 3 min; 13°C min-1 for 5 min; 1.5°C min-1 for 27 min; 5°C min-1 for 12 min and a final isotherm of 10 min. Nitrogen gas was used as carrier with a flow rate of 50 ml.min-1 and detection was done by a FID set at 250°C.
This work was partly supported by Sanofi Aventis (French), which provided the strain CA10/pCD63 and partly carried out under the project Futurol. Authors thank OSEO Innovation for its participation in the project Futurol funding, and C.O.N.A.C.Y.T. (Mexico) for financial doctoral support of Mr. Feria-Gervasio.
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