Over-production of Thermus protease in dense culture of Escherichia coli using two carbon sources

Escherichia coli JM109(DE3) harboring expression plasmid pkAQNÆC30, which carries the Thermus protease aqualysin I (AQI) gene, was cultivated with glucose as a sole carbon source. The final cell concentration was over 15 g dry weight/l and the amount of AQI produced reached approximately 130 kU/ml broth. Moreover, by using two carbon sources, glucose and glycerol, the production yield was increased to over 200 kU AQI/ml, while suppressing the formation of inhibitory acetic acid.     

Propionic acid fermentation from glycerol: comparison with conventional substrates

Instead of the conventional carbon sources used for propionic acid biosynthesis, the utilization of glycerol is considered here, since the metabolic pathway involved in the conversion of glycerol to propionic acid is redox-neutral and energetic. Three strains, Propionibacterium acidipropionici, Propionibacterium acnes and Clostridium propionicum were tested for their ability to convert glycerol to propionic acid during batch fermentation with initially 20 g/l glycerol. P. acidipropionici showed higher efficiency in terms of fermentation time and conversion yield than did the other strains. The fermentation profile of this bacterium consisted in propionic acid as the major product (0.844 mol/mol), and in minimal by-products: succinic (0.055 mol/mol), acetic (0.023 mol/mol) and formic (0.020 mol/mol) acids and n-propanol (0.036 mol/mol). The overall propionic acid productivity was 0.18 g l⁻¹h⁻¹. A comparative study with glucose and lactic acid as carbon sources showed both less diversity in end-product composition and a 17% and 13% lower propionic acid conversion yield respectively than with glycerol. Increasing the initial glycerol concentration resulted in an enhanced productivity up to 0.36 g l⁻¹h⁻¹ and in a maximal propionic acid concentration of 42 g/l, while a slight decrease of the conversion yield was noticed. Such a propionic acid production rate was similar or higher than the values obtained with lactic acid (0.35 g l⁻¹h⁻¹) or glucose (0.28 g l⁻¹h⁻¹). These results demonstrated that glycerol is a carbon source of interest for propionic acid production. Received: 15 July 1996 / Received revision: 11 November 1996 / Accepted: 11 November 1996     

Influence of acetic acid on the growth of Escherichia coli K12 during high-cell-density cultivation in a dialysis reactor

High-cell-density cultivations of Escherichia coli K12 in a dialysis reactor with controlled levels of dissolved oxygen were carried out with different carbon sources: glucose and glycerol. Extremely high cell concentrations of 190 g/l and 180 g/l dry cell weight were obtained in glucose medium and in glycerol medium respectively. Different behaviour was observed in the formation of acetic acid in these cultivations. In glucose medium, acetic acid was formed during the earlier phase of cultivation. However, in glycerol medium, acetic acid formation started later and was particularly rapid at the end of the cultivation. In order to estimate the influence of acetic acid during these high-cell-density cultivations, the inhibitory effect of acetic acid on cell growth was investigated under different culture conditions. It was found that the inhibition of cell growth by acetic acid in the fermentor was much less than that in a shaker culture. On the basis of the results obtained in these investigations of the inhibitory effect of acetic acid, and the mathematical predictions of cell growth in a dialysis reactor, the influence of acetic acid on high-cell-density cultivation is discussed. Received: 20 May 1997 / Received revision: 12 August 1997 / Accepted: 25 August 1997     

Propionic acid fermentation of glycerol and glucose by Propionibacterium acidipropionici and Propionibacterium freudenreichii ssp.shermanii

A comparative study was carried out in anaerobic batch cultures on 20 g/l of either glycerol or glucose using two propionibacteria strains, Propionibacterium acidipropionici and Propionibacterium freudenreichii ssp. shermanii. In all cases, fermentation end-products were the same and consisted of propionic acid as the major product, acetic acid as the main by-product and two minor metabolites, n-propanol and succinic acid. Evidence was provided that greater production of propionic acid by propionibacteria was obtained with glycerol as carbon and energy sources. P. acidipropionici showed higher efficiency in glycerol conversion to propionic acid with a faster substrate consumption (0.64 g l⁻¹ h⁻¹) and a higher propionic acid production (0.42 g l⁻¹ h⁻¹ and 0.79 mol/mol). The almost exclusive production of propionic acid from glycerol by this bacterium suggested an homopropionic tendency of this fermentation. Acetic acid final concentration was two times lower on glycerol (2 g/l) than on glucose (4 g/l) for both micro-organisms. P. freudenreichii ssp. shermanii exhibited a glycerol fermentation pattern typical of non-associated glycerol-consumption-product formation. This could indicate a particular metabolism for P. freudenreichii ssp. shermanii oriented towards the production of other specific components. These results tend to show that glycerol could be an excellent alternative to conventional carbon sources such as carbohydrates for propionic acid production. Received: 21 May 1999 / Accepted: 1 November 1999     

Culture medium containing glucose and glycerol as a mixed carbon source improves ε-poly-<Emphasis Type="SmallCaps">l</Emphasis>-lysine production by <Emphasis Type="Italic">Streptomyces</Emphasis> sp. M-Z18

To improve the efficiency of ε-poly-l-lysine (ε-PL) production by Streptomyces sp. M-Z18, batch and fed-batch fermentations with glucose and glycerol (co-fermentations) were performed. The batch fermentations showed that the initial ratio of glucose to glycerol plays an important role in glucose/glycerol co-fermentation. The optimal glucose/glycerol weight ratio was 30/30; this resulted in a maximum ε-PL productivity of 5.26 g/L/d. Glucose and glycerol were consumed synergistically during the co-fermentation process, and the length of time during which the substrate was exhausted was significantly shortened compared with the single carbon source fermentation. Under optimized conditions, fed-batch fermentations with glucose and glycerol as a mixed carbon source achieved maximum ε-PL concentration and productivity values of 35.14 g/L and 4.85 g/L/d, respectively. These values were respectively 1.43- and 1.39-, and 1.17- and 1.16-folds higher than those obtained from fermentations with glucose and glycerol as single carbon sources. The present study is the first to suggest that glucose/glycerol co-fermentation may be an efficient strategy for ε-PL production by Streptomyces sp. M-Z18.     

Role of the C-terminal pro-domain of aqualysin I in the maturation and translocation of the precursor across the cytoplasmic membrane in Escherichia coli

Aqualysin I, which is a subtilisin-type, extracellular protease secreted by Thermus aquaticus YT-1, is synthesized as a unique precursor bearing pro-domains at both N- and C-terminus of the mature protease domain as well as an N-terminal signal peptide. To investigate the function of the C-terminal pro-domain in maturation and export pathway of the precursor in E. coli cells, aqualysin I variants were constructed in which deletion mutants of the C-terminal pro-domain lacking its own signal peptide were inserted into pIN-III-ompA3. When E. coli harboring wild type and mutant plasmids were induced by 0.2 mM IPTG, active aqualysin I was produced by heat treatment at 65 °C. Aqualysin I precursors with deletions of more than 5 amino acid residues at the C-terminal end of pro-domain were much more rapidly processed than that of wild type, indicating that the C-terminal pro-domain functions as a inhibitor for processing of aqualysin I precursor. With the wild type, most of aqualysin I was present in membrane fraction (probably the outer membrane), whereas for the truncated mutants, it remained in the cytoplasm, indicating that for deletion mutants, their precursors expressed in cells were not translocated across the cytoplasmic membrane, despite the existence of an N-terminal signal peptide.     

Optimization of docosahexaenoic acid production by Schizochytrium limacinum SR21

Culture conditions of Schizochytrium limacinum SR21 for the purpose of microbial docosahexaenoic acid (DHA) production were investigated. The strain SR21 showed a wide tolerance to salinity; that is, the optimum salinity was between 50% and 200% that of sea water. Monosaccharides (glucose and fructose) and glycerol supported good cell growth and DHA yield. Di- and polysaccharides, oleic acid, and linseed oil gave low DHA yields. A high content of DHA (more than 30% of total fatty acids) was obtained from culture on glucose, fructose, and glycerol, and also the strain had simple polyunsaturated fatty acid profiles. The major polyunsaturated fatty acids other than DHA were n-6 docosapentaenoic acid only, and the contents of icosapentaenoic acid and arachidonic acid were less than 1%. Using corn steep liquor as a nitrogen source, a high total fatty acid content was obtained. The total fatty acid content in the dry cell weight increased as the concentration of the nitrogen source decreased, reached more than 50%. An increase in carbon source concentration led to a high DHA yield. A maximum DHA yield of more than 4 g/l was obtained in both glucose and glycerol media at 9% and 12% respectively. S. limacinum SR21 was thought to be a promising resource for microbial DHA production yielding a good level of productivity as well as a simple polyunsaturated fatty acid profile. Received: 26 June 1997 / Received revision: 29 August 1997  / Accepted: 19 September 1997     

Process development for production of recombinant human insulin-like growth factor-I in Escherichia coli

Fed-batch cultures were carried out to overproduce human insulin-like growth factor I (IGF-I) in Escherichia coli. The effects of carbon sources (glucose or glycerol) and induction time on cell growth and IGF-I production were investigated in more detail. Glycerol was a better carbon source than glucose for IGF-I production in fed-batch culture. Induction at the mid-exponential phase with glycerol as a carbon source in the pH-stat fed-batch culture was optimal for IGF-I production. Under this condition, 2.8 g L⁻¹ of fusion IGF-I was produced as inclusion bodies. We have also developed downstream processing for preparative scale purification of IGF-I from the fusion protein produced by the fed-batch culture using glycerol as a carbon source. After the fusion protein expressed was solubilized in 8 M urea and cleaved with hydroxylamine, the released IGF-I was purified by cation exchange chromatography, refolding and preparative scale reverse phase HPLC (rp-HPLC) to give recombinant IGF-I of >98% purity. The biological activities of the purified IGF-I were measured and found to be identical to those of commercial IGF-I. Journal of Industrial Microbiology & Biotechnology (2000) 24, 94–99. Received 13 January 1999/ Accepted in revised form 02 October 1999     

Metabolic flux analysis of Gluconacetobacter xylinus for bacterial cellulose production

Metabolic flux analysis was used to reveal the metabolic distributions in Gluconacetobacter xylinus (CGMCC no. 2955) cultured on different carbon sources. Compared with other sources, glucose, fructose, and glycerol could achieve much higher bacterial cellulose (BC) yields from G. xylinus (CGMCC no. 2955). The glycerol led to the highest BC production with a metabolic yield of 14.7 g/mol C, which was approximately 1.69-fold and 2.38-fold greater than that produced using fructose and glucose medium, respectively. The highest BC productivity from G. xylinus CGMCC 2955 was 5.97 g BC/L (dry weight) when using glycerol as the sole carbon source. Metabolic flux analysis for the central carbon metabolism revealed that about 47.96 % of glycerol was transformed into BC, while only 19.05 % of glucose and 24.78 % of fructose were transformed into BC. Instead, when glucose was used as the sole carbon source, 40.03 % of glucose was turned into the by-product gluconic acid. Compared with BC from glucose and fructose, BC from the glycerol medium showed the highest tensile strength at 83.5 MPa, with thinner fibers and lower porosity. As a main byproduct of biodiesel production, glycerol holds great potential to produce BC with superior mechanical and microstructural characteristics.     

Unique precursor structure of an extracellular protease, aqualysin I, with NH2- and COOH-terminal pro-sequences and its processing in Escherichia coli

Aqualysin I is a subtilisin-type serine protease which is secreted into the culture medium by Thermus aquaticus YT-1, an extremely thermophilic Gram-negative bacterium. The nucleotide sequence of the entire gene for aqualysin I was determined, and the deduced amino acid sequence suggests that aqualysin I is produced as a large precursor, consisting of at least three portions, an NH2-terminal pre-pro-sequence (127 amino acid residues), the protease (281 residues), and a COOH-terminal pro-sequence (105 residues). When the cloned gene was expressed in Escherichia coli cells, aqualysin I was not secreted. However, a precursor of aqualysin I lacking the NH2-terminal pre-pro-sequence (38-kDa protein) accumulated in the membrane fraction. On treatment of the membrane fraction at 65 degrees C, enzymatically active aqualysin I (28-kDa protein) was produced in the soluble fraction. When the active site Ser residue was replaced with Ala, cells expressing the mutant gene accumulated a 48-kDa protein in the outer membrane fraction. The 48-kDa protein lacked the NH2-terminal 14 amino acid residues of the precursor, and heat treatment did not cause any subsequent processing of this precursor. These results indicate that the NH2-terminal signal sequence is cleaved off by a signal peptidase of E. coli, and that the NH2- and COOH-terminal pro-sequences are removed through the proteolytic activity of aqualysin I itself, in that order. These findings indicate a unique four-domain structure for the aqualysin I precursor; the signal sequence, the NH2-terminal pro-sequence, mature aqualysin I, and the COOH-terminal pro-sequence, from the NH2 to the COOH terminus.     

Succinic acid production with reduced by-product formation in the fermentation of Anaerobiospirillum succiniciproducens using glycerol as a carbon source

Succinic acid was produced by fermentation of Anaerobiospirillum succiniciproducens using glycerol as a carbon source. When cells were anaerobically cultured in a medium containing 6.5 g/L glycerol, a high succinic acid yield (133%) was obtained while avoiding the formation of by-product acetic acid. The gram ratio of succinic acid to acetic acid was 25.8:1, which is 6.5 times higher than that obtained using glucose (ca. 4:1) as a carbon source. Therefore, succinic acid can be produced with much less by-product formation by using glycerol as a carbon source, which will facilitate its purification. When glucose and glycerol were cofermented with the increasing ratio of glucose to glycerol, the gram ratio of succinic acid to acetic acid and succinic acid yield decreased, suggesting that glucose enhanced acetic acid formation irrespective of the presence of glycerol. Glycerol consumption by A. succiniciproducens required unidentified nutritional components present in yeast extract. By intermittently feeding yeast extract along with glycerol, a high succinic acid yield (160%) could be obtained while still avoiding acetic acid formation. This resulted in the highest ratio of succinic acid to acetic acid (31.7:1).     

High-cell-density cultivation of the lipid accumulating yeast Cryptococcus curvatus using glycerol as a carbon source

 Cryptococcus curvatus is a yeast with industrial potential because it can grow and accumulate lipid on a very broad range of substrates. In this study we describe growth and lipid accumulation on glycerol in a fed-batch fermentation mode. We performed a fermentation consisting of two phases. The first phase is the biomass production phase in which there is no nutrient limitation except for very short periods of glycerol exhaustion. The substrate feed was controlled by the dissolved oxygen tension. In the second phase nitrogen limitation was introduced, which causes lipid accumulation. This way very high cell densities of 118 g/l in a 50-h fermentation could be reached. With a lipid production rate of 0.59 g lipid l^-1h^-1, a cellular lipid content of 25% was obtained. The growth and lipid accumulation phase are characterized by different cellular fatty acid compositions. In the growth phase, a relatively high amount of C18:2 (linoleic acid) is present, which is a major component of membrane lipids. C18:0 (stearic acid) and C18:1 (oleic acid) are major constituents of the accumulated triglycerides and therefore the relative amount of C18:2 decreases during the lipid accumulation phase. Received: 19 September 1995/Received revision: 28 December 1995/Accepted: 8 January 1996     

IPTG limitation avoids metabolic burden and acetic acid accumulation in induced fed-batch cultures of Escherichia coli M15 under glucose limiting conditions

The most common strategy to produce recombinant proteins using Escherichia coli as expression vector is fed-batch culture, since high cell density cultures strategies have successfully been applied. Several methodologies to limit the specific growth rate in order to control E. coli metabolism have been defined, demonstrating that cultures can be grown under glucose limitation up to high cell densities without accumulation of acetic acid. However, under induction conditions it has been observed that E. coli metabolism is reorganized again and leads to acetic acid accumulation, causing inhibition of cell growth and decreasing protein expression efficiency.We propose a double limitation strategy (glucose and IPTG) for E. coli fed-batch cultures to avoid the deregulation of the metabolism in the induction phase. Reducing the concentration of IPTG while keeping glucose growth limitation, the accumulation of acetic acid decreased. At an IPTG concentration of 0.03 mmol/g DCW no accumulation of acetic acid was observed during the induction phase, in contraposition to what has normally been observed.Although a slight reduction of protein expression rate was observed when applying this double limitation strategy, the bioprocess volumetric productivity was enhanced due to the capability to prolong the induction phase, reaching higher levels of protein production. Another advantage of this strategy is the reduction of media cost due to the lower level of IPTG used.     

Nucleotide sequence of the gene for aqualysin I (a thermophilic alkaline serine protease) of Thermus aquaticus YT-1 and characteristics of the deduced primary structure of the enzyme

Aqualysin I is an alkaline serine protease which is secreted into the culture medium by Thermus aquaticus YT-1, an extreme thermophile [Matsuzawa, H., Hamaoki, M. & Ohta, T. (1983) Agric. Biol. Chem. 47, 25-28]. The gene encoding aqualysin I was cloned into Escherichia coli using synthetic oligodeoxyribonucleotides as hybridization probes. The nucleotide sequence of the cloned DNA was determined. The primary structure of aqualysin I, deduced from the nucleotide sequence, agreed with the NH2-terminal sequence previously reported and the determined amino acid sequences, including the COOH-terminal sequence, of the tryptic peptides derived from aqualysin I. Aqualysin I comprised 281 amino acid residues and its molecular mass was determined to be 28,350. On alignment of the whole amino acid sequence, aqualysin I showed high sequence homology with the subtilisin-type serine proteases, and 43% identity with proteinase K, 37-39% with subtilisins and 34% with thermitase. Extremely high sequence identity was observed in the regions containing the active-site residues, corresponding to Asp32, His64 and Ser221 of subtilisin BPN'. The nucleotide sequence of the cloned DNA (1105 nucleotides) revealed that it contains the entire gene encoding aqualysin I and one open reading frame without a translational stop codon. Therefore, aqualysin I was considered to be produced as a large precursor, which contains a NH2-terminal portion, the protease and a COOH-terminal portion. The G + C content of the coding region for aqualysin I was 64.6%, which is lower than those of other Thermus genes (68-74%). The codon usage in the aqualysin I gene was rather random in comparison with that in other Thermus genes.     

Identification and production of a rhamnolipidic biosurfactant by a Pseudomonas species

 A glycolipid-producing bacterium, Pseudomonas aeruginosa GL1, was isolated from the soil contaminated with polycyclic aromatic hydrocarbons (PAH) from a manufactured gas plant. The glycolipid produced was characterized in detail by chromatographic procedures as a mixture of four rhamnolipids, consisting of different associations of rhamnose and hydroxy fatty acids: the main component was monorhamnosyl di-3-hydroxydecanoic acid. The rhamnolipid composition presented marked analogies with a defined part of P. aeruginosa outer membrane lipopolysaccharides (lipopolysaccharide band A). Rhamnolipid production was stimulated under conditions of nitrogen limitation. Glycerol yielded higher productions than did hydrophobic carbon sources. Cell hydrophobicity decreased during growth on glycerol and on n-hexadecane whereas glycolipid production increased. P. aeruginosa GL1 was found to be unable to grow on a variety of 2, 3 and 4 cycle PAH. However, it was shown to persist after at least 12 subcultures in a bacterial population growing on a mixture of pure PAH, suggesting a physiological role for rhamnolipid as a means to enhance PAH availability in a mutualistic PAH-degrading bacterial community. Received: 4 July 1995/Received revision: 7 September 1995/Accepted: 13 September 1995     

A non-covalent NH2-terminal pro-region aids the production of active aqualysin I (a thermophilic protease) without the COOH-terminal pro-sequence in Escherichia coli

The precursor of aqualysin I, an extracellular protease produced by Thermus aquaticus, consists of four domains: an N-terminal signal peptide, an N-terminal pro-sequence, the protease domain and a C-terminal pro-sequence. In an Escherichia coli expression system, mature and active aqualysin I is formed by treatment at 65 degrees C and the N-pro-sequence is required for its production. Complete deletion of the C-pro-sequence did not affect the production of active aqualysin I, indicating that the C-pro-sequence is not essential. A non-covalent N-pro-region was separately synthesized from the protease domain with or without the C-pro-sequence. In this system, mature and active aqualysin I was detected only when the C-pro-sequence was deleted.     

Increase of lycopene production by supplementing auxiliary carbon sources in metabolically engineered <Emphasis Type="Italic">Escherichia coli</Emphasis>

In the fed-batch culture of glycerol using a metabolically engineered strain of Escherichia coli, supplementation with glucose as an auxiliary carbon source increased lycopene production due to a significant increase in cell mass, despite a reduction in specific lycopene content. l-Arabinose supplementation increased lycopene production due to increases in cell mass and specific lycopene content. Supplementation with both glucose and l-arabinose increased lycopene production significantly due to the synergistic effect of the two sugars. Cell growth by the consumption of carbon sources was related to endogenous metabolism in the host E. coli. Supplementation with l-arabinose stimulated only the mevalonate pathway for lycopene biosynthesis and supplementation with both glucose and l-arabinose stimulated synergistically only the mevalonate pathway. In the fed-batch culture of glycerol with 10 g l⁻¹ glucose and 7.5 g l⁻¹ l-arabinose, the cell mass, lycopene concentration, specific lycopene content, and lycopene productivity after 34 h were 42 g l⁻¹, 1,350 mg l⁻¹, 32 mg g cells⁻¹, and 40 mg l⁻¹ h⁻¹, respectively. These values were 3.9-, 7.1-, 1.9-, and 11.7-fold higher than those without the auxiliary carbon sources, respectively. This is the highest reported concentration and productivity of lycopene.     

Comparison of citric acid production from glycerol and glucose by different strains of <Emphasis Type="Italic">Yarrowia lipolytica</Emphasis>

A wild type strain A-101 of Y. lipolytica and its three acetate-negative mutants (Wratislavia 1.31, Wratislavia AWG7, and Wratislavia K1) were compared for the production of citric acid from glucose and glycerol (pure and crude) in batch cultures. The substrates were used either as single carbon sources or as mixtures of glucose and pure or crude glycerol. The kinetic parameters, i.e., the volumetric citric acid production rate and yield obtained in the study show that the Wratislavia 1.31 and Wratislavia AWG7 strains produced the highest amount of citric acid from glycerol, with a yield from 0.40 to 0.53 g g⁻¹. This substrate was found to be a better carbon source for the biosynthesis of citric acid than glucose. The results obtained with the same strains have shown low content of isocitric acid and polyols, such as erythritol and mannitol. Y. lipolytica A-101 strain produced the highest amount of isocitric acid, from 13.8 to 21% isocitric acid in the sum of citric acids. However, the highest concentrations of erythritol were found in cultures with Y. lipolytica Wratislavia K1, from 18.1 to 30 g l⁻¹, for glucose and pure glycerol, respectively.     

Regulation of lysine ɛ-aminotransferase by carbon source and lack of control by phosphate in Streptomyces clavuligerus

Cephalosporin production by Streptomyces clavuligerus is known to be negatively regulated by carbon sources, e.g., glycerol and starch, and by phosphate at high concentrations. Formation of lysine ɛ-aminotransferase (LAT) activity, the first enzyme of the biosynthetic pathway, was affected by a high concentration of carbon source. Whereas 3% starch more than doubled LAT activity production as compared to 1% starch, 3% glycerol repressed LAT activity formation by 20%–30%. LAT activity production was not affected by 100 mM K₂HPO₄. Our results thus show that the negative effects of 2% glycerol and 3% starch and 100 mM phosphate on cephalosporin production are not due to an effect on production of LAT activity. However, repression of LAT activity by 3% glycerol would be expected to play a negative role in antibiotic production. Received: 13 June 1997 / Received revision: 20 August 1997 / Accepted: 25 August 1997     

Co-fermentation of carbon sources by Enterobacter aerogenes ATCC 29007 to enhance the production of bioethanol

We investigated the enhancement of bioethanol production in Enterobacter aerogenes ATCC 29007 by co-fermentation of carbon sources such as glycerol, glucose, galactose, sucrose, fructose, xylose, starch, mannitol and citric acid. Biofuel production increases with increasing growth rate of microorganisms; that is why we investigated the optimal growth rate of E. aerogenes ATCC 29007, using mixtures of different carbon sources with glycerol. E. aerogenes ATCC 29007 was incubated in media containing each carbon source and glycerol; growth rate and bioethanol production improved in all cases compared to those in medium containing glycerol alone. The growth rate and bioethanol production were highest with mannitol. Fermentation was carried out at 37 °C for 18 h, pH 7, using 50 mL defined production medium in 100 mL serum bottles at 200 rpm. Bioethanol production under optimized conditions in medium containing 16 g/L mannitol and 20 g/L glycerol increased sixfold (32.10 g/L) than that containing glycerol alone (5.23 g/L) as the carbon source in anaerobic conditions. Similarly, bioethanol production using free cells in continuous co-fermentation also improved (27.28 g/L) when 90.37 % of 16 g/L mannitol and 67.15 % of 20 g/L glycerol were used. Although naturally existing or engineered microorganisms can ferment mixed sugars sequentially, the preferential utilization of glucose to non-glucose sugars often results in lower overall yield and productivity of ethanol. Here, we present new findings in E. aerogenes ATCC 29007 that can be used to improve bioethanol production by simultaneous co-fermentation of glycerol and mannitol.