Improving intracellular production of recombinant protein in <Emphasis Type="Italic">Pichia pastoris</Emphasis> using an optimized preinduction glycerol-feeding scheme

High-cell-density production of recombinant growth hormone of Lateolabrax japonicus (rljGH) expressed intracellularly in Pichia pastoris was investigated. In the regular strategy of induction at a cell density of 160 g l⁻¹, short duration of intracellular rljGH accumulation (17 h) resulted in a low final cell density of 226 g l⁻¹. Thus, a novel strategy of induction at a cell density of 320 g l⁻¹ was investigated. In this strategy, the preinduction glycerol-feeding scheme had a significant effect on the post-induction production. Constant glycerol feeding led to a decrease of the specific rljGH production and specific production rate because of low preinduction specific growth rate. This decrease was avoided by exponential glycerol feeding to maintain a preinduction specific growth rate of 0.16 h⁻¹. The results from exponential glycerol feeding indicated that the rljGH production depended on the preinduction specific growth rate. Moreover, mixed feeding of methanol and glycerol during induction improved the specific production rate to 0.07 mg g⁻¹ h⁻¹ from 0.043 mg g⁻¹ h⁻¹. Consequently, both high cell density (428 g l⁻¹) and high rljGH production could be achieved by the novel strategy: growing the cells at the specific growth rate of 0.16 h⁻¹ to the cell density of 320 g l⁻¹ and inducing the expression by mixed feeding.     

Enhanced l-lysine production in threonine-limited continuous culture of Corynebacterium glutamicum by using gluconate as a secondary carbon source with glucose

In order to improve the production rate of l-lysine, a mutant of Corynebacterium glutamicum ATCC 21513 was cultivated in complex medium with gluconate and glucose as mixed carbon sources. In a batch culture, this strain was found to consume gluconate and glucose simultaneously. In continuous culture at dilution rates ranging from 0.2 h⁻¹ to 0.25 h⁻¹, the specific l-lysine production rate increased to 0.12 g g⁻¹ h⁻¹ from 0.1 g g⁻¹ h⁻¹, the rate obtained with glucose as the sole carbon source [Lee et al. (1995) Appl Microbiol Biotechnol 43:1019–1027]. It is notable that l-lysine production was observed at higher dilution rates than 0.4 h⁻¹, which was not observed when glucose was the sole carbon source. The positive effect of gluconate was confirmed in the shift of the carbon source from glucose to gluconate. The metabolic transition, which has been characterized by decreased l-lysine production at the higher glucose uptake rates, was not observed when gluconate was added. These results demonstrate that the utilization of gluconate as a secondary carbon source improves the maximum l-lysine production rate in the threonine-limited continuous culture, probably by relieving the limiting factors in the lysine synthesis rate such as NADPH supply and/or phosphoenolpyruvate availability. Received: 16 May 1997 / Received revision: 28 August 1997 / Accepted: 29 August 1997     

Two-stage glycerol feeding for enhancement of recombinant hG-CSF production in a fed-batch culture of Pichia pastoris

Recombinant hG-CSF was expressed in Pichia pastoris under the control of the AOX1 promoter. In this study, the glycerol feeding rate was adjusted to achieve the maximum attainable specific growth rate before induction. Using a two-stage glycerol feeding method, the specific growth rate was changed from a maximum value of 0.21 h⁻¹ (at the beginning of feeding) to 0.15 h⁻¹ prior to induction. With this approach, the final dry cell wt and rhG-CSF yield achieved was close to 120 g l⁻¹ and 320 mg l⁻¹, respectively. Our study found that the two-stage feeding method allowed the overall productivity of rhG-CSF to increase 2.9 times that of the conventional fed-batch method.     

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.     

Production of lipase by high cell density fed-batch culture of Candida cylindracea

Candida cylindracea NRRL Y-17506 was grown to produce extracellular lipase from oleic acid as a carbon source. Through flask cultures, it was found that the optimum initial oleic acid concentration for cell growth was 20 g l⁻¹. However, high initial concentrations of oleic acid up to 50 g l⁻¹ were not inhibitory. The highest extracellular lipase activity obtained in flask culture was 3.0 U ml⁻¹ after 48 h with 5 g l⁻¹ of initial oleic acid concentration. Fed-batch cultures (intermittent and stepwise feeding) were carried out to improve cell concentration and lipase activity. For the intermittent feeding fed-batch culture, the final cell concentration was 52 g l⁻¹ and the extracellular lipase activity was 6.3 U ml⁻¹ at 138.5 h. Stepwise feeding fed-batch cultures were carried out to simulate an exponential feeding and to investigate the effects of specific growth rate (0.02, 0.04 and 0.08 h⁻¹) on cell growth and lipase production. The highest final cell concentration obtained was 90 g l⁻¹ when the set point of specific growth rate (μ_set) was 0.02 h⁻¹. High specific growth rate (0.04 and 0.08 h⁻¹) decreased extracellular lipase production in the later part of fed-batch cultures due to build-up of the oleic acid oversupplied. The highest extracellular lipase activity was 23.7 U ml⁻¹ when μ_set was 0.02 h⁻¹, while the highest lipase productivity was 0.31 U ml⁻¹ h⁻¹ at μ_set of 0.08 h⁻¹.     

Lactic acid production from xylose by the fungus Rhizopus oryzae

Lignocellulosic biomass is considered nowadays to be an economically attractive carbohydrate feedstock for large-scale fermentation of bulk chemicals such as lactic acid. The filamentous fungus Rhizopus oryzae is able to grow in mineral medium with glucose as sole carbon source and to produce optically pure l(+)-lactic acid. Less is known about the conversion by R. oryzae of pentose sugars such as xylose, which is abundantly present in lignocellulosic hydrolysates. This paper describes the conversion of xylose in synthetic media into lactic acid by ten R. oryzae strains resulting in yields between 0.41 and 0.71 g g⁻¹. By-products were fungal biomass, xylitol, glycerol, ethanol and carbon dioxide. The growth of R. oryzae CBS 112.07 in media with initial xylose concentrations above 40 g l⁻¹ showed inhibition of substrate consumption and lactic acid production rates. In case of mixed substrates, diauxic growth was observed where consumption of glucose and xylose occurred subsequently. Sugar consumption rate and lactic acid production rate were significantly higher during glucose consumption phase compared to xylose consumption phase. Available xylose (10.3 g l⁻¹) and glucose (19.2 g l⁻¹) present in a mild-temperature alkaline treated wheat straw hydrolysate was converted subsequently by R. oryzae with rates of 2.2 g glucose l⁻¹ h⁻¹ and 0.5 g xylose l⁻¹ h⁻¹. This resulted mainly into the product lactic acid (6.8 g l⁻¹) and ethanol (5.7 g l⁻¹).     

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     

Glucoamylase production in batch, chemostat and fed-batch cultivations by an industrial strain of Aspergillus niger

The Aspergillus niger strain BO-1 was grown in batch, continuous (chemostat) and fed-batch cultivations in order to study the production of the extracellular enzyme glucoamylase under different growth conditions. In the pH range 2.5–6.0, the specific glucoamylase productivity and the specific growth rate of the fungus were independent of pH when grown in batch cultivations. The specific glucoamylase producivity increased linearly with the specific growth rate in the range 0–0.1 h⁻¹ and was constant in the range 0.1–0.2 h⁻¹. Maltose and maltodextrin were non-inducing carbon sources compared to glucose, and the maximum specific growth rate was 0.19 ± 0.02 h⁻¹ irrespective of whether glucose or maltose was the carbon source. In fed-batch cultivations, glucoamylase titres of up to 6.5 g l⁻¹ were obtained even though the strain contained only one copy of the glaA gene. Received: 5 May 1999 / Received revision: 7 September 1999 / Accepted: 17 September 1999     

Production of high-density Chlorella culture grown in fermenters

The freshwater microalga Chlorella vulgaris was grown heterotrophically in fed-batch 50–600-L fermenters at 36°C, on aerated and mixed nutrient solution with urea as a nitrogen and glucose as a carbon and energy source. Cell density increased from the initial value 6.25 to 117.18 g DW L⁻¹ in 32 h in the fermenter 50 L at a mean growth rate 3.52 g DW L⁻¹ h⁻¹. The DW increase in the fermenter 200 L was from 7.25 to 94.82 g DW L⁻¹ in 26.5 h at a mean growth rate 3.37 g DW L⁻¹ h⁻¹. Mean specific growth rate μ was about 0.1 h⁻¹ in the both fermenters, if nutrients and oxygen were adequately supplied. The DW increase in the fermenter 600 L was from 0.8 to 81.6 g DW L⁻¹ in 66.5 h at a mean growth rate 1.22 g DW L⁻¹ h⁻¹ and μ = 0.07 h⁻¹. A limitation of the cell growth rate in 600 L fermenter caused by a low dissolved oxygen concentration above cell densities higher than 10 g DW L⁻¹) occurred. Specific growth rate decreased approximately linearly with increasing glucose concentration (25–80 g glucose L⁻¹) at the beginning of cultivation and decreased with the time of cultivation. The cell yield was 0.55–0.69 g DW (g glucose)⁻¹. The content of proteins, β-carotene, and chlorophylls in the cells steadily increased and starch content decreased, by keeping aerated and mixed culture another 12 h in fermenter after the cell growth was stopped due to glucose deficiency.     

Production of 1,3-propanediol by Klebsiella pneumoniae from glycerol broth

Broth containing 152 g glycerol l⁻¹ from Candida krusei culture was converted to 1,3-propanediol by Klebsiella pneumoniae. Residual glucose in the broth promoted growth of K. pneumoniae while acetate was inhibitory. After desalination treatment of glycerol broth by electrodialysis, the acetate in the broth was removed. A fed-batch culture with electrodialytically pretreated broth as␣substrate was developed giving 53 g 1,3- propanediol l⁻¹ with a yield of 0.41 g g⁻¹ glycerol and a productivity of 0.94 g l⁻¹ h⁻¹.     

Production of 1,3-propanediol by Clostridium butyricum in continuous culture with cell recycling

The continuous fermentation of 1,3-propanediol from glycerol by Clostridium butyricum was subjected to cell recycling by filtration using hollow-fibre modules made from polysulphone. The performance of the culture system was checked at a retention ratio (dilution rate/bleed rate) of 5, dilution rates between 0.2 h⁻¹ and 1.0 h⁻¹ and glycerol input concentrations of 32 g l⁻¹ and 56 g l⁻¹. The near-to-optimum propanediol concentration of 26.5 g l⁻¹ (for 56 g l⁻¹ glycerol) was maintained up to a dilution rate of 0.5 h⁻¹ and then decreased while the propanediol productivity was highest at 0.7 h⁻¹. The productivity could be increased by a factor of four in comparison to the continuous culture without cell recycling. By application of the model of Zeng and Deckwer [(1995) Biotechnol Prog 11: 71–79] for cultures under substrate excess, it was shown that the limitations resulted exclusively from product inhibition and detrimental influences from the cell recycling system, such as shear stress, were not involved. Received: 20 October 1997 / Received revision: 12 December 1997 / Accepted: 14 December 1997     

Performance assessment of malolactic fermenting bacteria Oenococcus oeni and Lactobacillus brevis in continuous culture

The growth performance of malolactic fermenting bacteria Oenococcus oeni NCIMB 11648 and Lactobacillus brevis X₂ was assessed in continuous culture. O. oeni grew at a dilution rate range of 0.007 to 0.052 h⁻¹ in a mixture of 5:6 (g l⁻¹) of glucose/fructose at an optimal pH of 4.5, and L. brevis X₂ grew at 0.010 to 0.089 h⁻¹ in 10 g l⁻¹ glucose at an optimal pH of 5.5 in a simple and safe medium. The cell dry weight, substrate uptake and product formation were monitored, as well as growth kinetics, yield parameters and fermentation balances were also evaluated under pH control conditions. A comparison of growth characteristics of two strains was made, and this showed significantly different performance. O. oeni has lower maximum specific growth rate (μ_max=0.073 h⁻¹), lower maximum cell productivity (Q _x ^max=17.6 mg cell l⁻¹ h⁻¹), lower maximum biomass yield (Y _x/s ^max=7.93 g cell mol⁻¹ sugar) and higher maintenance coefficient (m _s=0.45 mmol⁻¹ sugar g⁻¹ cell h⁻¹) as compared with L. brevis X₂ (μ_max=0.110 h⁻¹; Q _x ^max=93.2 g⁻¹ cell mol⁻¹ glucose; Y _x/s ^max=22.3 g cell mol⁻¹ glucose; m _s=0.21 mmol⁻¹ glucose g⁻¹ cell h⁻¹). These data suggest a possible more productive strategy for their combined use in maturation of cider and wine.     

Production of 1,3-Propanediol by Clostridium butyricum VPI 3266 in continuous cultures with high yield and productivity

The effects of dilution rate and substrate feed concentration on continuous glycerol fermentation by Clostridium butyricum VPI 3266, a natural 1,3-propanediol producer, were evaluated in this work. A high and constant 1,3-propanediol yield (around 0.65 mol/mol), close to the theoretical value, was obtained irrespective of substrate feed concentration or dilution rate. Improvement of 1,3-propanediol volumetric productivity was achieved by increasing the dilution rate, at a fixed feed substrate concentration of 30, 60 or 70 g l⁻¹. Higher 1,3-propanediol final concentrations and volumetric productivities were also obtained when glycerol feed concentration was increased from 30 to 60 g l⁻¹, at D=0.05–0.3 h⁻¹, and from 60–70 g l⁻¹, at D=0.05 and 0.1 h⁻¹·30 g l⁻¹ of 1,3-propanediol and the highest reported value of productivity, 10.3 g l⁻¹ h⁻¹, was achieved at D=0.30 h⁻¹ and 60 g l⁻¹ of feed glycerol. A switch to an acetate/butyrate ratio higher than one was observed for 60 g l⁻¹ of feed glycerol and a dilution rate higher than 0.10 h⁻¹; moreover, at D=0.30 h⁻¹ 3-hydroxypropionaldehyde accumulation was observed for the first time in the fermentation broth of C. butyricum.     

Effect of growth rate on the production of<Emphasis Type="SmallCaps">l</Emphasis>-proline in the fed-batch culture of<Emphasis Type="Italic">Corynebacterium acetoacidophilum</Emphasis>

Corynebacterium acetoacidophilum RYU3161 was cultivated in al-histidine-limited fed-batch culture. To investigate the effect of cell growth on thel-proline production, 5l fed-batch culture was performed using an exponential feeding rate to obtain the specific growth rates (μ) of 0.04, 0.06, 0.08, and 0.1 h⁻¹. The results show that the highest production ofl-proline was obtained at μ=0.04 h⁻¹. The specificl-proline production rate (Q_p) increased proportionally as a function of the specific growth rate, but decreased after it revealed the maximum value at μ=0.08 h⁻¹. Thus, the highest productivity ofl-proline was 1.66 g L⁻¹ h⁻¹ at μ=0.08 h⁻¹. The results show that the production of L-proline inC. acetoacidophilum RYU3161 has mixed growth-associated characteristics.     

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     

Bioconversion of isopropanol by a solvent tolerant Sphingobacterium mizutae strain

The bioconversion of high concentration isopropanol (2-propanol, IPA) was investigated by a solvent tolerant strain of bacteria, which was identified as Sphingobacterium mizutae ST2 by partial 16S rDNA gene sequencing. This strain of bacteria exhibited the ability to utilise high concentration isopropanol as the sole carbon source, with mineralization occurring via an acetone intermediate into central metabolism. The biodegradative performance of this strain for IPA was examined over a 2–38 g l⁻¹ concentration range, using specific growth rate (μ) and conversion rate analysis. Maximum specific growth rates (μ_max) of 0.0045 h⁻¹ were routinely obtainable on IPA. In addition, the highest specific IPA degradation rate was obtained at a concentration of 7.5 g l⁻¹ with a corresponding value of 0.045 g IPA g cells⁻¹ h⁻¹. While the highest acetone yield reached its maximum value of 0.940 g acetone g IPA⁻¹ at 7.5 g IPA l⁻¹. This is the first report on bioconversion of isopropanol at such high concentration by this solvent tolerant strain of S. mizutae and may allow its application in novel biocatalytic processes for effective biological conversion in two-phase solvent systems.     

Continuous butanol production with reduced byproducts formation from glycerol by a hyper producing mutant of <Emphasis Type="Italic">Clostridium pasteurianum</Emphasis>

Butanol, a four-carbon primary alcohol (C₄H₁₀O), is an important industrial chemical and has a good potential to be used as a superior biofuel. Bio-based production of butanol from renewable feedstock is a promising and sustainable alternative to substitute petroleum-based fuels. Here, we report the development of a process for butanol production from glycerol, which is abundantly available as a byproduct of biodiesel production. First, a hyper butanol producing strain of Clostridium pasteurianum was isolated by chemical mutagenesis. The best mutant strain, C. pasteurianum MBEL_GLY2, was able to produce 10.8 g l⁻¹ butanol from 80 g l⁻¹ glycerol as compared to 7.6 g l⁻¹ butanol produced by the parent strain. Next, the process parameters were optimized to maximize butanol production from glycerol. Under the optimized batch condition, the butanol concentration, yield, and productivity of 17.8 g l⁻¹, 0.30 g g⁻¹, and 0.43 g l⁻¹ h⁻¹ could be achieved. Finally, continuous fermentation of C. pasteurianum MBEL_GLY2 with cell recycling was carried out using glycerol as a major carbon source at several different dilution rates. The continuous fermentation was run for 710 h without strain degeneration. The acetone–butanol–ethanol productivity and the butanol productivity of 8.3 and 7.8 g l⁻¹ h⁻¹, respectively, could be achieved at the dilution rate of 0.9 h⁻¹. This study reports continuous production of butanol with reduced byproducts formation from glycerol using C. pasteurianum, and thus could help design a bioprocess for the improved production of butanol.     

Microbial production of 1,3-propanediol by Klebsiella pneumoniae using crude glycerol from biodiesel preparations

1,3-Propanediol (1,3-PD) was produced by Klebsiella pneumoniae using crude glycerol obtained from biodiesel production. The 1,3-PD concentration of 51.3 g/l⁻¹ on crude glycerol from alkali-catalyzed methanolysis of soybean oil was comparable to that of 53 g/l⁻¹ on crude glycerol derived from a lipase-catalyzed process. The productivities of 1.7 g l⁻¹ h⁻¹ on crude glycerol were comparable to that of 2 g l⁻¹ h⁻¹ on pure glycerol. It could be concluded that the crude glycerol could be directly converted to 1,3-PD without any prior purification.     

Lactic acid production from cellulosic waste by immobilized cells of Lactobacillus delbrueckii

Industrial waste corn cob residue (from xylose manufacturing) without pretreatment was hydrolyzed by cellulase and cellobiase. The cellulosic hydrolysate contained 52.4 g l⁻¹ of glucose and was used as carbon source for lactic acid fermentation by cells of Lactobacillus delbrueckii ZU-S2 immobilized in calcium alginate gel beads. The final concentration of lactic acid and the yield of lactic acid from glucose were 48.7 g l⁻¹ and 95.2%, respectively, which were comparative to the results of pure glucose fermentation. The immobilized cells were quite stable and reusable, and the average yield of lactic acid from glucose in the hydrolysate was 95.0% in 12 repeated batches of fermentation. The suitable dilution rate of continuous fermentation process was 0.13 h⁻¹, and the yield of lactic acid from glucose and the productivity were 92.4% and 5.746 g l⁻¹ h⁻¹, respectively. The production of lactic acid by simultaneous saccharification and fermentation (SSF) process was carried out in a coupling bioreactor, the final concentration of lactic acid was 55.6 g l⁻¹, the conversion efficiency of lactic acid from cellulose was 91.3% and the productivity was 0.927 g l⁻¹ h⁻¹. By using fed-batch technique in the SSF process, the final concentration of lactic acid and the productivity increased to 107.6 g l⁻¹ and 1.345 g l⁻¹ h⁻¹, respectively, while the dosage of cellulase per gram substrate decreased greatly. This research work should advance the bioconversion of renewable cellulosic resources and reduce environmental pollution.     

1,3-Propanediol production in a two-step process fermentation from renewable feedstock

In this work, the production of 1,3-propanediol from glucose and molasses was studied in a two-step process using two recombinant microorganisms. The first step of the process is the conversion of glucose or other sugar into glycerol by the metabolic engineered Saccharomyces cerevisiae strain HC42 adapted to high (>200 g l⁻¹) glucose concentrations. The second step, carried out in the same bioreactor, was performed by the engineered strain Clostridium acetobutylicum DG1 (pSPD5) that converts glycerol to 1,3-propanediol. This two-step strategy led to a flexible process, resulting in a 1,3-propanediol production and yield that depended on the initial sugar concentration. Below 56.2 g l⁻¹ of sugar concentration, cultivation on molasses or glucose showed no significant differences. However, at higher molasses concentrations, glycerol initially produced by yeast could not be totally converted into 1,3-propanediol by C. acetobutylicum and a lower 1,3-propanediol overall yield was observed. In our hand, the best results were obtained with an initial glucose concentration of 103 g l⁻¹, leading to a final 1,3-propanediol concentration of 25.5 g l⁻¹, a productivity of 0.16 g l⁻¹ h⁻¹ and 1,3-propanediol yields of 0.56 g g⁻¹ glycerol and 0.24 g g⁻¹ sugar, which is the highest value reported for a two-step process. For an initial sugar concentration (from molasses) of 56.2 g l⁻¹, 27.4 g l⁻¹ of glycerol were produced, leading to 14.6 g l⁻¹ of 1.3-propanediol and similar values of productivity, 0.15 g l⁻¹ h⁻¹, and overall yield, 0.26 g g⁻¹ sugar.