Engineering of acetyl-CoA metabolism for the improved production of polyhydroxybutyrate in Saccharomyces cerevisiae
© Kocharin et al.; licensee Springer. 2012
Received: 8 September 2012
Accepted: 12 September 2012
Published: 25 September 2012
Through metabolic engineering microorganisms can be engineered to produce new products and further produce these with higher yield and productivities. Here, we expressed the bacterial polyhydroxybutyrate (PHB) pathway in the yeast Saccharomyces cerevisiae and we further evaluated the effect of engineering the formation of acetyl coenzyme A (acetyl-CoA), an intermediate of the central carbon metabolism and precursor of the PHB pathway, on heterologous PHB production by yeast. We engineered the acetyl-CoA metabolism by co-transformation of a plasmid containing genes for native S. cerevisiae alcohol dehydrogenase (ADH2), acetaldehyde dehydrogenase (ALD6), acetyl-CoA acetyltransferase (ERG10) and a Salmonella enterica acetyl-CoA synthetase variant (acsL641P), resulting in acetoacetyl-CoA overproduction, together with a plasmid containing the PHB pathway genes coding for acetyl-CoA acetyltransferase (phaA), NADPH-linked acetoacetyl-CoA reductase (phaB) and poly(3-hydroxybutyrate) polymerase (phaC) from Ralstonia eutropha H16. Introduction of the acetyl-CoA plasmid together with the PHB plasmid, improved the productivity of PHB more than 16 times compared to the reference strain used in this study, as well as it reduced the specific product formation of side products.
Poly-(R)-3-hydroxybutyrate (PHB) is the most common type of polyhydroxyalkanoates (PHAs) synthesized and accumulated by microorganisms like Ralstonia eutropha (also known as Cupriavidus necator, Wautersia eutropha, Alcaligenes eutrophus), Bacillus megaterium or Pseudomonas sp. as carbon and energy storage material in response to conditions of physiological stress (Steinbuchel et al. 1993). Biodegradable PHB is a linear polyester consisting solely of the stereospecific monomer, (R)-3-hydroxybutyric acid. It belongs to the group of short chain length PHAs consisting of C3-C5 hydroxyacid monomers. (Hankermeyer and Tjeerdema 1999; Melchiors et al. 1994). The biosynthesis pathway of PHB involves three enzymes and their sequential reactions (Breuer et al. 2002; Carlson et al. 2002; Steinbüchel 2001; Steinbüchel and Hein 2001). The first enzyme of the pathway is acetyl-CoA C-acetyltransferase [EC 188.8.131.52], encoded by phaA, which catalyzes the condensation of two acetyl-CoA molecules to form acetoacetyl-CoA (Peoples and Sinskey 1989b). The next step is the reduction of acetoacetyl-CoA to (R)-3-hydroxybutyryl-CoA, which is catalyzed by NADPH-dependent acetoacetyl-CoA reductase [EC 184.108.40.206] encoded by phaB (Peoples and Sinskey 1989b). Finally, PHA synthase [EC 2.3.1.-] encoded by phaC, catalyzes the polymerization of (R)-3-hydroxybutyryl-CoA monomers to PHB (Peoples and Sinskey 1989a).
The natural PHB producers like R. eutropha, Bacillus megaterium or Pseudomonas sp. are known to produce and accumulate PHB as a storage compound in response to nutrient imbalance caused by growth under conditions of carbon source excess but limitation in other essential nutrients (Steinbüchel and Hein 2001; Trotsenko and Belova 2000). Instead of employing the natural PHB producers, which can depolymerize PHB and use it as a secondary energy source, metabolic engineering can be used to transfer the PHB biosynthetic pathway to alternative hosts that may have advantage over the natural PHB producers, in particular the lack of enzymes for PHB depolymerization (Uchino and Saito 2006). Furthermore, by transferring to alternative hosts one may take advantage of a range of technologies developed for general platform cell factories like Escherichia coli and Saccharomyces cerevisiae. Thus, there have been a range of studies where PHB production has been evaluated in E. coli and further metabolic engineering has been carried out with the objective to improve the productivity. In a metabolic and kinetic study, a recombinant E. coli strain producing PHB was examined and compared to the native PHB producer, R. eutropha, and this study revealed that the PHB flux was highly sensitive to the acetyl-CoA/CoA ratio, the total acetyl-CoA plus CoA concentration and pH (van Wegen et al. 2001). In recombinant E. coli, a mutation in arcA encoding a protein that regulates aerobic respiration under microaerobic conditions resulted in higher amounts of PHB accumulated in the cell (Nikel et al. 2006). Low-agitation conditions had a positive effect on PHB synthesis from glycerol in recombinant E. coli carrying the phaCAB operon and phaP encoding a granule-associated protein (phasin) (de Almeida et al. 2010). Several studies also attempted to synthesize PHB in plants according to the aim to produce high amounts of PHB at lower costs compared to microbial fermentation, particularly in plant plastids where the biosynthesis of fatty acids from acetyl-CoA occurs (Bohmert et al. 2000; Nawrath et al. 1994; Petrasovits et al. 2012). However, the growth of some of these transgenic plants was inhibited, possibly due to the metabolic burden of PHB synthesis (Poirier et al. 1992).
The benefits of using S. cerevisiae as a model for producing PHB is that the molecular machinery of S. cerevisiae is well studied and as the most widely used eukaryal microorganism for industrial production of fuels and chemicals it is an attractive cell factory platform. Furthermore, its genome has been very well characterized and genome scale metabolic models have been reconstructed (Goffeau 2000; Nookaew et al. 2008). For these reasons, several attempts have been made to evaluate S. cerevisiae as a cell factory for PHB production (Breuer et al. 2002; Dimster-Denk and Rine 1996; Leaf et al. 1996; Marchesini et al. 2003; Zhang et al. 2006). Synthesis of PHB in S. cerevisiae has initially been demonstrated by expressing only bacterial polyhydroxybutyrate synthase (Leaf et al. 1996). This PHB synthesis approach is successful because of the activity of native thiolase and reductase enzymes involved in the synthesis of D-3-hydroxybutyryl-CoA in S. cerevisiae. However, the yield obtained in this study was very low when compared with the expression of all three genes of the PHB biosynthesis pathway (Breuer et al. 2002; Carlson et al. 2002; Carlson and Srienc 2006). Thiolase enzymes in S. cerevisiae exist and function in three different compartments, in mitochondria and peroxisomes for fatty acid β-oxidation and in the cytoplasm for the mevalonate pathway (Hiser et al. 1994). However, only the cytoplasmic thiolase participates in PHB biosynthesis. Many approaches have been followed to improve the production of PHB in yeast. Srienc and co-workers performed elementary mode analysis of a S. cerevisiae containing the PHB synthesis pathway in order to identify new metabolic engineering targets (Carlson et al. 2002). The analysis suggested that the introduction of the ATP citrate-lyase reaction and the transhydrogenase reaction can improve the theoretical PHB carbon yield (Carlson et al. 2002). Acetyl-CoA serves as the precursor for the PHB biosynthesis pathway and increasing the availability of acetyl-CoA was proposed to improve PHB production (Carlson and Srienc 2006; Suzuki et al. 2002). However, using enzyme inhibitors to reduce its consumption by other pathways or feeding of the substrate during cultivation would result in increasing production costs and may not be feasible for industrial applications. Here, we demonstrated metabolic pathway engineering by co-transformation of a plasmid containing the PHB biosynthesis pathway and an acetyl-coenzyme A (acetyl-CoA) boost plasmid designated to improve the availability of cytoplasmic acetyl-CoA and hereby improve the productivity of PHB in S. cerevisiae.
Materials and methods
Strains, media, and culture conditions
Plasmids were maintained and propagated in E. coli DH5α. The preparation of competent E. coli cells and their transformation were performed according to standard protocols (Sambrook and Russell 2006). Lysogeny broth (LB) medium was used for routine culturing of E. coli (Bertani 1951) and 80 mg L-1 ampicillin was added to LB when needed. S. cerevisiae strain CEN.PK113-11C (MAT a SUC2 MAL2 8cura3 52 his3-Δ1; provided by P. Kötter, Frankfurt, Germany) was used as the background strain for evaluation of the polyhydroxybutyrate pathway. Plasmid containing yeast strains were selected on synthetic dextrose (SD) medium, prepared with 6.7 g L-1 yeast nitrogen base without amino acids (YNB-AA) (Formedium, Hunstanton, UK) and 20 g L-1 glucose with complete supplement mixture (CSM) lacking uracil and/or histidine (Formedium) where appropriate.
Plasmid construction and yeast transformation
Oligonucleotides used in this study
Sequence (5' -3')
Yeast strains and plasmids used in this study
Genotype or relevant feature(s)
MAT a SUC2 MAL2-8cura3-52 his3-Δ1
MAT a SUC2 MAL2-8cura3-52 his3-Δ1
MAT a SUC2 MAL2-8cura3-52 his3-Δ1
MAT a SUC2 MAL2-8cura3-52 his3-Δ1 cit2Δ
(Chen et al. 2012)
MAT a SUC2 MAL2-8cura3-52 his3-Δ1 mls1Δ
(Chen et al. 2012)
MAT a SUC2 MAL2-8cura3-52 his3-Δ1 cit2Δ
MAT a SUC2 MAL2-8cura3-52 his3-Δ1 mls1Δ
Shake flask cultivation
The pre-cultures for shake flask cultivations were prepared by inoculation of 5 mL modified minimal medium in a 14 mL culture tube and grown at 30°C and 180. The modified minimal medium for shake flask cultivations was prepared as follows: 5 g⋅L-1 (NH4)2SO4; 3 g⋅L-1 KH2PO4; 0.5 g⋅L-1 MgSO4⋅7H2O; 1 mL⋅L-1 of trace metal solution and vitamin solution (see below) with an initial pH of 6.5. 45 mL of defined minimal medium in a 100 mL unbaffled flask were inoculated with an amount of pre-culture that resulted in a final optical density of 0.02 at 600 nm (OD600). The culture was grown at 30°C with 180 rpm in an orbital shaking incubator and samples were taken at 40, 80 and 120 h to determine PHB production.
PHB production was evaluated in defined minimal media with the following composition: 5 g⋅L-1 (NH4)2SO4; 3 g L-1 KH2PO4; 0.5 g L-1 MgSO4⋅7H2O; 1 mL L-1 trace metal solution (pH 4.0: 15.0 g L-1 EDTA (sodium salt); 0.45 g L-1 ZnSO4⋅7H2O; 1 g L-1 MnCl2⋅2H2O; 0.3 g L-1 CoCl2⋅6H2O; 0.3 g L-1 CuSO4⋅5H2O; 0.4 g L-1 Na2MoO4⋅2H2O; 0.45 g L-1 CaCl2⋅2H2O; 0.3 g L-1 FeSO4⋅7H2O; 0.1 g L-1 H3BO3, and 0.10 g L-1 KI). The pH was adjusted to 5 by adding 2 M KOH and autoclaved separately from the carbon source solution. Glucose was added at a concentration of 20 g L-1. Vitamin solution (pH 6.5: 0.05 g L-1 biotin; 0.2 g L-1 ρ-amino benzoic acid; 1 g L-1 nicotinic acid; 1 g L-1 Ca-pantothenate; 1 g L-1 pyridoxine-HCl; 1 g L-1 thiamine-HCl and 25 g L-1 myo-inositol) was filter sterilized and aseptically added to the medium after autoclaving at the concentration of 1 mL L-1. Batch cultivations were carried out in 1.2 L bioreactors. The pre-cultures were prepared using the same culture conditions as for shake flask cultivation. 700 mL of defined minimal medium were inoculated with an amount of pre-culture that resulted in a final OD600 of 0.02. The temperature was kept at 30°C and the pH was adjusted to 5.00 ± 0.05 using 2 M KOH.
Culture samples of 10 mL volume were centrifuged at 5,311 × g and 4°C for 5 min and the pellets were washed once with distilled water and centrifuged at 14,000 × g for 1 min. To lyophilize the biomass, the recovered cell pellet was immediately frozen by immersion in liquid nitrogen followed by lyophilization under vacuum (Christ Alpha 2–4 LSC, Shropshire, UK). The cell dry weight was determined and the pellet kept at 4°C for further analysis.
Metabolites including glucose, ethanol, glycerol, and acetate were quantified in the culture supernatant using an Ultimate 3000 HPLC (Dionex, Sunnyvale, CA, USA) equipped with an Aminex HPX 87 H ion exclusion column (300 mm × 7.8 mm, Bio-Rad Laboratories, Hercules, CA, USA) which was operated at 45°C and a flow rate of 0.6 mL min-1 of 5 mM H2SO4 using a refractive index detector and UV detector for analysis of sugars and organic acids, respectively.
PHB was analyzed as described previously (Karr et al. 1983; Tyo et al. 2006). 10–20 mg of dried cells were weighed and boiled in 1 mL of concentrated sulfuric acid for 60 min and then diluted with 4 mL of 14 mM H2SO4. Samples were centrifuged (15 min, 16,000 × g) to remove cell debris, and the supernatant was analyzed using an Ultimate 3000 HPLC (Dionex) equipped with an Aminex HPX-87 H ion exclusion column (300 × 7.8 mm; Bio-Rad Laboratories) and UV detector. Commercially available PHB (Sigma-Aldrich, St. Louis, MO), processed in parallel with the samples, was used as a standard. The HPLC was operated at 60°C and a flow rate of 0.6 mL min-1 of 5 mM H2SO4.
The total lipid extraction method was adapted from Bligh and Dyer (Bligh and Dyer 1959). Briefly, 15 mg of freeze-dried cell pellets were treated with 1 unit μL-1 zymolyase in 1 mL digestion buffer (1.2 M glycerol, 100 mM sodium thioglycolate, 50 mM Tris-sulfate, pH 7.5) at 37°C for 15 min, followed by centrifugation at 3000 rpm for 3 min. The mixture of collected spheroplasts was spiked with cholesterol as internal standard, 7 ml of chloroform:methanol (2:1, v/v) were added and shaken vigorously at room temperature and 500 rpm for 30 min. 1.7 mL of 0.73% NaCl was added to the mixture prior centrifugation at 3500 rpm for 5 min at 4°C. The lower (organic) phase was collected and the upper phase was re-extracted with 5 mL of chloroform-methanol (85:15 v/v). The lower (organic) phase was collected and pooled with the previous organic fraction and kept at −20°C for further HPLC analysis.
Lipid separation and quantification were performed using the method modified from Silversand and Haux (Silversand and Haux 1997). Lipid separation was accomplished using an Ultimate 3000 HPLC (Dionex) equipped with a Corona charged aerosol detector (CAD) (Dionex) connected with nitrogen gas at 35 psi gas pressure. A 20 μL volume of each sample was injected into a Luna 5 μm HILIC 200 Å 250 × 4.6 mm LC column (Phenomenex, Torrance, CA). The flow-rate was 0.8 mL⋅min-1 and the column temperature was kept at 25°C during all runs. A gradient flow with 3 solvents (solvent A, 99:1 by vol. of hexane/acetic acid, solvent B 70:29:1, by vol. of hexane/isopropanol/acetic acid, solvent C 85:14:1, by vol. of isopropanol/water/acetic acid) was applied for the separation of lipids. Triethylamine (0.08%) was added to solvent B and solvent C for better separation. The HPLC system was equilibrated with 99% solvent A. The gradient profile started from 3% solvent B at 7 min, reached 10% solvent B in 1 min and ended at 100% solvent B in 15 min, while solvent C was kept at 0% from 0 min to 15 min. This gradient profile is used for separation of triacylglycerol (TAG), free fatty acids, cholesterol (as internal standard) and ergosterol. After 15 min, solvent A was kept at 0% until 35 min. Meanwhile, an increase of solvent C to 65% from 15 min to 32 min was applied for separation of phospholipids (phosphatidylethanolamine, phosphatidylinositol, phosphatidylcholine, phosphatidylserine, phosphatidic acid). After that, solvent C was decreased to 0% from 32 min to 35 min and 100% solvent B was applied to the system. After 40 min, 99% solvent A was run for 5 min in order to equilibrate and stabilize the system for the measurement of the next sample. A logarithmic plot of peak area versus the concentration of each lipid standard was used to generate a calibration curve. The slope determined from the log-log plot was further used for lipid quantification (Nair and Werling 2009).
Characterization of PHB-producing S. cerevisiae
CIT2 encoding peroxisomal citrate synthase catalyzes the conversion of oxaloacetate and acetyl-CoA to citrate and plays role in acetate metabolism. MLS1 encoding malate synthase catalyzes the conversion of glyoxylate and acetyl-CoA to malate in the glyoxylate shunt. Deletion of CIT2 and MLS1 affect the integrity of the glyoxylate shunt and will therefore reduce the drain of acetyl-CoA through this pathway and hereby possibly affect the availability of cytosolic acetyl-CoA. Thus, the effect of CIT2 and MLS1 deletion on PHB production was also investigated. The biomass yield of cit2Δ (SCKK009) was less than that of mls1Δ (SCKK010), and the biomass yield for both the deletion strains were lower than those of the non-deletion reference strain without the acetyl-CoA plasmid (SCKK005) and the non-deletion strain with the acetyl-CoA plasmid (SCKK006) (see Figure 2a). The biomass yield of the deletion strains, SCKK009 and SCKK010, was lower than that of non-deletion strains, SCKK005 and SCKK006, due to the impaired C2 carbon utilization. The recombinant strain with both the acetyl-CoA boost plasmid and the PHB plasmid (SCKK006) produced an 18 times higher final concentration of PHB (at 120 h) compared to the reference strain, SCKK005 (Figure 2b). Besides that, the amount of accumulated PHB in SCKK009 and SCKK010 was less than SCKK006. Although, mls1Δ (SCKK010) gave lower biomass yield than the reference, it gave higher PHB titer compare to the non-deletion reference strain (SCKK005) when the deletion strain carried the acetyl-CoA plasmid. This result showed the combined effect of mls1Δ together with the utilization of acetyl-CoA plasmid on the availability of acetyl-CoA and the influence of the deletion on PHB production. The consumption rate of ethanol in the deletion strains, especially in cit2Δ (SCKK009), was slower than for the non-deletion strain as the residual amount of ethanol was detected after 80 h of cultivation (Figure 2c). In addition, more than 6.5 g L-1 of acetate was detected in the medium after 120 of fermentation of SCKK009, which is clear evidence for the impaired C2 metabolism. Due to the negative impact of CIT2 and MLS1 deletion on growth and PHB production, the recombinant strains SCKK005 and SCKK006 without gene deletions were selected for further characterization in bioreactors.
Yields and kinetic parameters obtained from batch cultivations
Maximum specific growth rate
0.27 ± 0.02
0.28 ± 0.00
Glucose consumption rate
g (g DW h)-1
1.80 ± 0.09
2.24 ± 0.33
Biomass yield on glucose
g (g glc)-1
0.15 ± 0.01
0.13 ± 0.02
Ethanol yield on glucose
g (g glc)-1
0.35 ± 0.05
0.35 ± 0.07
Glycerol yield on glucose*
g (g glc)-1
0.05 ± 0.00
0.07 ± 0.00
Acetate yield on glucose*
g (g glc)-1
0.02 ± 0.00
PHB yield on glucose*
mg (g glc)-1
0.02 ± 0.01
0.13 ± 0.02
Biomass yield on ethanol
g (g EtOH)-1
0.46 ± 0.27
0.45 ± 0.08
PHB yield on ethanol*
mg (g EtOH)-1
0.22 ± 0.04
6.09 ± 1.44
Comparison of specific productivities in pathway engineered strains
The addition of precursor molecules to the fermentation medium has been shown to improve the formation of many biological products, e.g. supplementation with glucosamine as precursor resulted in improved hyaluronic acid production by E. coli (Mao et al. 2009) and supplementation with specific amino acids enhanced heterologous protein production by S. cerevisiae (Görgens et al. 2005). Extra feeding of acetate (0.5 g⋅L-1 with pH adjusted to 4.5) and panthothenate (1000 μg⋅L-1) as a precursors of acetyl-CoA were tested by Carlson and Srienc in order to increase PHB accumulation in S. cerevisiae (Carlson and Srienc 2006). Feeding a combination of acetate and pantothenate was found to improve PHB production by approximately 45% over the control. Instead of feeding precursors to improve the productivity, which would increase the costs of PHB production, we focused on pathway engineering to increase the supply of the precursor for PHB production and hereby improve the economic feasibility of a process using S. cerevisiae.
The native ADH2 in S. cerevisiae is a glucose-repressible alcohol dehydrogenase. It catalyzes the oxidation of ethanol to acetaldehyde only when glucose becomes depleted from the medium. In order to activate the reaction catalyzed by ADH2 when glucose was completely consumed, the HXT7 promoter was selected to control ADH2 in the acetyl-CoA plasmid. Although the HXT7 promoter is a glucose-repressible promoter, we select the HXT7 promoter based on its strong expression level especially during the ethanol phase. Therefore, ADH2 under control of the HXT7 promoter ensures the conversion of ethanol to acetyldehyde and is responsible for the initial step in the utilization of ethanol as carbon source. ALD6 encoding cytosolic aldehyde dehydrogenase is involved in the conversion of acetaldehyde to acetate. This enzyme utilizes NADP+ as the preferred coenzyme. As a result, ALD6 over-expression might help providing NADPH, a required cofactor for PHB production (Boubekeur et al. 2001). There are two acetyl-CoA synthetase in S. cerevisiae, encoded by ACS1 and ACS2. Both of these enzymes catalyze ATP-dependent activation of acetate to acetyl-CoA. The expression of ACS1 is subjected to glucose repression while ACS2 can be expressed during growth on glucose where it is likely to be responsible for cytosolic acetyl-CoA production. However, the regulation of both enzymes is complex and hence over-expression is believed necessary to increase the flux towards acetyl-CoA. In the native host Salmonella enterica, mutations at Leu-641 of acetyl CoA synthetase (Acs), prevent the acetylation by acetyltransferase bypassing the need for sirtuin deacetylase activity and maintain the enzyme in an active state during growth on acetate. (Starai et al. 2005). Enhancing acetyl-CoA supply by engineering the pyruvate dehydrogenase bypass through over-expression of acetaldehyde dehydrogenase in combination with introduction of a S. enterica acetyl CoA synthetase variant (L641P) in S. cerevisiae, was successful demonstrated to improve the productivity of isoprenoids in yeast (Shiba et al. 2007).
CIT2, the peroxisomal citrate synthase and MLS1, the cytosolic malate synthase are key enzymes of the glyoxylate shunt and hereby affect acetate metabolism (Kunze et al. 2006; Lee et al. 2011). Deletion of CIT2 and MLS1 in order to improve the availability of cytosolic acetyl-CoA was investigated for its impact on PHB production. However, this deletion strategy resulted in the impaired metabolism due to the incapability to utilize C2 carbon via the glyoxylate shunt in cit2Δ and mls1Δ strains. The deletion strains have only the tricarboxylic acid cycle (TCA cycle) to utilize C2 carbon for energy production whereas the biosynthesis of C4 dicarboxylic acids required as precursors for amino acids biosynthesis cannot take place, resulting in lack of growth (Chen et al. 2012). This is reflected by a much reduced biomass yield in the cit2Δ strain. In the mls1Δ strain (SCKK009), less acetate was accumulated in the medium compared to the cit2Δ strain and acetate was slowly consumed until the end of fermentation. This might be due to the activity of the homolog malate synthase encoded by DAL7 (Hartig et al. 1992). Moreover, the deletion of CIT2 affect acetate metabolism and reduced the efficiency of acetyl-CoA synthetase, both native acetyl-CoA synthetase and the additional acetyl-CoA synthetase, to catalyze the ATP-dependent activation of acetate to acetyl-CoA thus resulting in more than 6.5 g/L-1 of acetate accumulated in the cit2Δ strain and no further biomass production after glucose is completely consumed (after 24 hr). Besides that, the PHB titer was drastically decreased as compared to the non-deletion strain, SCKK006.
The comparison of the specific productivities in the PHB producing strains revealed that employing the acetyl-CoA boost plasmid helps in directing carbon towards the PHB pathway. Although, there was a difference in PHB yield when the PHB strains, SCKK005 and SCKK006, were cultivated in bioreactors. This might be explained by the cultivation condition in the bioreactor which favors the growth of S. cerevisiae rather than PHB production. Thus, the maximum specific growth rate in shake flasks was 0.18-0.20 h-1 while the maximum specific growth rate in the bioreactors was 0.27-0.28 h-1. Although the PHB yield from the bioreactors was less than shake flask cultivation the difference in PHB productivity between SCKK005 and SCKK006 clearly showed the effect of employing the acetyl-CoA plasmid for PHB production. Therefore, the flux from glucose to PHB was analyzed by using the information from aerobic batch bioreactor cultivations. For this analysis free fatty acids, TAG, phospholipids and ergosterol were considered as side products of PHB production. From this analysis we found that over-expression of ERG10 together with phaA significantly reduced the specific productivities of TAG and phospholipids as side products compared to the reference strain which does not have over-expression of ERG10. Although increased production of acetyl-CoA might lead to fatty acid or lipid synthesis, our study show that when the cells contain a heterologous pathway to PHB flux is actually directed towards PHB rather than towards lipids. Thus, we can conclude that enhancement of acetyl-CoA production by co-expression of genes on the acetyl-CoA boost plasmid improved the productivity of PHB during growth on glucose and further enhanced the productivity of PHB approximately 16.5 times bioreactor cultivations and reduce the flux from acetyl-CoA to lipids.
We thank Chalmers Foundation and the Knut and Alice Wallenberg Foundation for funding part of this work. We also acknowledge the Thailand Science and Technology Ministry for providing a stipend to KK.
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