Xylitol production from a mutant strain of Candida tropicalis

Aims: To characterize the kinetics of growth, sugar uptake and xylitol production in batch and fed‐batch cultures for a xylitol assimilation‐deficient strain of Candida tropicalis isolated via chemical mutagenesis. Methods and Results: Chemical mutagenesis using nitrosoguanidine led to the isolation of the xylitol‐assimilation deficient strain C. tropicalis SS2. Shake‐flask fermentations with this mutant showed a sixfold higher xylitol yield than the parent strain in medium containing 25 g l^?1 glucose and 25 g l^?1 xylose. With 20 g l^?1 glycerol, replacing glucose for cell growth, and various concentrations of xylose, the studies indicated that the mutant strain resulted in xylitol yields from xylose close to theoretical. Under fully aerobic conditions, fed‐batch fermentation with repeated addition of glycerol and xylose resulted in 3·3 g l^?1 h^?1 xylitol volumetric productivity with the final concentration of 220 g l^?1 and overall yield of 0·93 g g^?1 xylitol. Conclusions: The xylitol assimilation‐deficient mutant isolated in this study showed the potential for high xylitol yield and volumetric productivity under aerobic conditions. In the evaluation of glycerol as an alternative low‐cost nonfermentable carbon source, high biomass and xylitol yields under aerobic conditions were achieved; however, the increase in initial xylose concentrations resulted in a reduction in biomass yield based on glycerol consumption. This may be a consequence of the role of an active transport system in the yeast requiring increasing energy for xylose uptake and possible xylitol secretion, with little or no energy available from xylose metabolism. Significance and Impact of the Study: The study confirms the advantage of using a xylitol assimilation‐deficient yeast under aerobic conditions for xylitol production with glycerol as a primary carbon source. It illustrates the potential of using the xylose stream in a biomass‐based bio‐refinery for the production of xylitol with further cost reductions resulting from using glycerol for yeast growth and energy production.     

Multi-copy expression and fed-batch production of Rhodotorula araucariae epoxide hydrolase in Yarrowia lipolytica

Epoxide hydrolases (EHs) of fungal origin have the ability to catalyze the enantioselective hydrolysis of epoxides to their corresponding diols. However, wild type fungal EHs are limited in substrate range and enantioselectivity. Additionally, the production of fungal epoxide hydrolase (EH) by wild-type strains is typically very low. In the present study, the EH-encoding gene from Rhodotorula araucariae was functionally expressed in Yarrowia lipolytica, under the control of a growth phase inducible hp4d promoter, in a multi-copy expression cassette. The transformation experiments yielded a positive transformant, with a final EH activity of 220 U/g dw in shake-flask cultures. Evaluation of this transformant in batch fermentations resulted in ~ 7-fold improvement in EH activity over the flask scale. Different constant specific feed rates were tested in fed-batch fermentations, resulting in an EH activity of 1,750 U/g dw at a specific feed rate of ~ 0.1 g/g/h, in comparison to enzyme production levels of 0.3 U/g dw for the wild type R. araucariae and 52 U/g dw for an Escherichia coli recombinant strain expressing the same gene. The expression of EH in Y. lipolytica using a multi-copy cassette demonstrates potential for commercial application.     

Production of citric acid with immobilized Yarrowia lipolytica

Summary Citric acid was produced with immobilized Yarrowia lipolytica yeast in repeated batch-shake-flask and air-lift fermentations. In active and passive immobilization methods calcium alginate, -carrageenan, polyurethane gel, nylon web and polyurethane foams were tested as carriers in repeated-batch fermentations. The highest citric acid productivity of 155 mg l^–1 h^–1 was reached with alginate-bead-immobilized cells in the first batch. A decrease in bead diameter from 5–6 mm to 2–3 mm increased the volumetric citric acid productivity threefold. In an air-lift bioreactor the highest citric acid productivity of 120 mg l^–1 h^–1 with a product concentration of 16.4 g l^–1 was obtained with cells immobilized in -carrageenan beads. Offprint requests to: H. Kautola     

Production of a sterol esterase from Ophiostoma piceae in batch and fed‐batch bioprocesses using different Pichia pastoris phenotypes as cell factory

The potential biotechnological applications for the Ophiostoma piceae sterol esterase (OPE) are conditioned to the availability of high enzyme amounts at low prices. This enzyme is a versatile biocatalyst with different biotechnological applications. In this work a systematic study on its heterologous production in different Pichia pastoris strains and operational strategies is presented. The best results were obtained using an AOX1 defective yeast strain in a fed‐batch bioprocess using methanol as inducer substrate at a set point of 2.5 g L^?1 and sorbitol as cosubstrate by means of a preprogramed exponential feeding rate at a μ = 0.02 h^?1, reaching 30 U mL^?1 of enzyme and a volumetric productivity of 403.5 U L^?1 h^?1. These values are twofold higher than those obtained with a Mut⁺ phenotype using methanol a sole carbon source. OPE was the main protein secreted by the yeast, 55% for Mut^s versus 25% for Mut^+. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:1012–1020, 2014     

α-Ketoglutaric acid production from rapeseed oil by Yarrowia lipolytica yeast

The possibility of using rapeseed oil as a carbon source for microbiological production of α-ketoglutaric acid (KGA) has been studied. Acid formation on the selective media has been tested in 26 strains of Yarrowia lipolytica yeast, and the strain Y. lipolytica VKM Y-2412 was selected as a prospective producer of KGA from rapeseed oil. KGA production by the selected strain was studied in dependence on thiamine concentration, medium pH, temperature, aeration, and concentration of oil. Under optimal conditions (thiamine concentration of 0.063 μg?g cells^?1, pH?3.5, 30 °C, high dissolved oxygen concentration (pO₂) of 50 % (of air saturation), and oil concentration in a range from 20 to 60 g?l^?1), Y. lipolytica VKM Y-2412 produced up to 102.5 g?l^?1 of KGA with the mass yield coefficient of 0.95 g?g^?1 and the volumetric KGA productivity (Q _KGA) of 0.8 g?l^?1?h^?1.     

Production of high ethanol concentrations from glucose using a vertical rotating immobilized cell reactor of the bacterium zymomonas mobilis

Long-term continuous ethanol production of up to 80 g.l¹ with a volumetric ethanol productivity of 63 g. l^?1. h^?1 was maintained for more than 72 days using a Vertical Rotating Immobilized Cell Reactor of the bacterium Z. mobilis. Continuous production of higher ethanol concentration was unsuccessful due to an inhibition of cell growth by long exposure to high ethanol concentrations. However, ethanol concentration as high as 120g. l^?1 and volumetric ethanol productivity of 13g. l^?1. h^?1 were achieved in a repeated-batch fermentation system using the same bioreactor. By a simple washing operation at the end of each run, immobilized biomass could be effectively regenerated and used to carry out more than 10 successive fermentation cycles.     

Enhanced yield of medium-chain-length polyhydroxyalkanoates from nonanoic acid by co-feeding glucose in carbon-limited, fed-batch culture

Medium-chain-length polyhydroxyalkanoates (MCL-PHAs) were produced in carbon-limited, single-stage, fed-batch fermentations of Pseudomonas putida KT2440 by co-feeding nonanoic acid (NA) and glucose (G) to enhance the yield of PHA from NA. An exponential (μ = 0.25 h⁻¹) followed by a linear feeding strategy at a NA:G ratio of 1:1 (w/w) achieved 71 g l⁻¹ biomass containing 56% PHA. Although the same overall PHA productivity (1.44 g l⁻¹ h⁻¹) was obtained when NA alone was fed at the same specific growth rate, the overall yield of PHA from NA increased by 25% (0.66 g PHA g NA⁻¹ versus 0.53 g g⁻¹) with glucose co-feeding. Further increasing glucose in the feed (NA:G = 1:1.5) resulted in a slightly higher yield (0.69 g PHA g NA⁻¹) but lower PHA content (48%) and productivity (1.16 g l⁻¹ h⁻¹). There was very little change in the PHA composition.     

Kinetic model-based feed-forward controlled fed-batch fermentation of Lactobacillus rhamnosus for the production of lactic acid from Arabic date juice

Arabic date is overproduced in Arabic countries such as Saudi Arabia and Iraq and is mostly composed of sugars (70–80 wt%). Here we developed a fed-batch fermentation process by using a kinetic model for the efficient production of lactic acid to a high concentration from Arabic date juice. First, a kinetic model of Lactobacillus rhamnosus grown on date juice in batch fermentation was constructed in EXCEL so that the estimation of parameters and simulation of the model can be easily performed. Then, several fed-batch fermentations were conducted by employing different feeding strategies including pulsed feeding, exponential feeding, and modified exponential feeding. Based on the results of fed-batch fermentations, the kinetic model for fed-batch fermentation was also developed. This new model was used to perform feed-forward controlled fed-batch fermentation, which resulted in the production of 171.79 g l^?1 of lactic acid with the productivity and yield of 1.58 and 0.87 g l^?1 h^?1, respectively.     

Use of ceramic-based cell immobilization to produce 1,3-propanediol from biodiesel-derived waste glycerol with Klebsiella pneumoniae

Aims: The feasibility of the continuous production of a valuable bioplastic raw material, namely 1,3‐propanediol (1,3‐PDO) from biodiesel by‐product glycerol, using immobilized cells was investigated. In addition, the effect of hydraulic retention time (HRT) was also analysed. Methods and Results: Ceramic balls and ceramic rings were used for the immobilization of a locally isolated strain; Klebsiella pneumoniae (GenBank no. 27F HM063413 ). HRT of 1 h is the best one in terms of volumetric production rate (g 1,3‐PDO l^?1 h^?1). The results indicated that ceramic‐based cell immobilization achieved a 2‐fold higher production rate (10 g 1,3‐PDO l^?1 h^?1) in comparison with suspended cell system (4·9 g 1,3‐PDO l^?1 h^?1). Conclusions: Continuous cultures with immobilized cells revealed that 1,3‐PDO production was more effective and more stable than suspended culture systems. Furthermore, cell immobilization had also obvious benefits especially for resistance of the production for extreme conditions (high organic loading rates, cell washouts). The results were important for understanding the significance of continuous immobilization process among other well‐known 1,3‐PDO fermentation processes. Significance and Impact of the Study: This work is a promising process for further studies, as the immobilized micro‐organism was able to reach high volumetric production rates at short HRT, it has an important role in tolerating and converting glycerol during fermentation. Therefore, HRT is a very significant operational parameter (P value <0·05) directly affecting the bioreactor performance and production rate.     

Metabolism in 1,3‐propanediol fed‐batch fermentation by a D‐lactate deficient mutant of Klebsiella pneumoniae

Klebsiella pneumoniae HR526, a new isolated 1,3‐propanediol (1,3‐PD) producer, exhibited great productivity. However, the accumulation of lactate in the late‐exponential phase remained an obstacle of 1,3‐PD industrial scale production. Hereby, mutants lacking D ‐lactate pathway were constructed by knocking out the ldhA gene encoding fermentative D ‐lactate dehydrogenase (LDH) of HR526. The mutant K. pneumoniae LDH526 with the lowest LDH activity was studied in aerobic fed‐batch fermentation. In experiments using pure glycerol as feedstock, the 1,3‐PD concentrations, conversion, and productivity increased from 95.39 g L^?1, 0.48 and 1.98 g L^?1 h^?1 to 102. 06 g L^?1, 0.52 mol mol^?1 and 2.13 g L^?1 h^?1, respectively. The diol (1,3‐PD and 2,3‐butanediol) conversion increased from 0.55 mol mol^?1 to a maximum of 0.65 mol mol^?1. Lactate would not accumulate until 1,3‐PD exceeded 84 g L^?1, and the final lactate concentration decreased dramatically from more than 40 g L^?1 to <3 g L^?1. Enzymic measurements showed LDH activity decreased by 89–98% during fed‐batch fermentation, and other related enzyme activities were not affected. NADH/NAD⁺ enhanced more than 50% in the late‐exponential phase as the D ‐lactate pathway was cut off, which might be the main reason for the change of final metabolites concentrations. The ability to utilize crude glycerol from biodiesel process and great genetic stability demonstrated that K. pnemoniae LDH526 was valuable for 1,3‐PD industrial production. Biotechnol. Bioeng. 2009; 104: 965–972. © 2009 Wiley Periodicals, Inc.     

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.     

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.     

Microbial production of 2,3-butanediol by a newly-isolated strain of Serratia marcescens

A newly-isolated strain of Serratia marcescens, G12, was characterized for 2,3-butanediol (2,3-BD) production. In shake-flask and batch fermentations, 2,3-BD reached 48.5 and 51 g l^?1, respectively. Low amounts of (~8 g l^?1) of acetoin were also formed. In fed-batch fermentations, strain G12 produced 72.8 g 2,3-BD l^?1 with glucose initially at 130 g l^?1. When aeration rate was increased to 2.5 vvm for the fermentation process, 2,3-BD reached 87.8 g l^?1 and the highest productivity was 1.6 g l^?1 h^?1. Acetoin was at 6.2 g l^?1. G12 therefore may be a suitable candidate strain for large-scale production of 2,3-BD.     

Poly(β-hydroxybutyric acid) thermoplastic production by Alcaligenes latus: Behavior of fed-batch cultures

Fed-batch culture of Alcaligenes latus, ATCC 29713, was investigated for producing the intracellular bioplastic poly(β–hydroxybutyric acid), PHB. Constant rate feeding, exponentially increasing feeding rate, and pH-stat fed batch methods were evaluated. pH-stat fed batch culture reduced or delayed accumulation of the substrate in the broth and led to significantly enhanced PHB productivity relative to the other modes of feeding. Presence of excessive substrate appeared to inhibit PHB synthesis, but not the production of cells. In fed-batch culture, the maximum specific growth rate (0.265?h^?1) greatly exceeded the value (0.075?h^?1) previously observed in batch culture of the same strain. Similarly, the maximum PHB production rate (up to 1.15?g?·?l^?1?·?h^?1) was nearly 8-fold greater than values observed in batch operations. Fed-batch operation was clearly superior to batch fermentation for producing PHB. A low growth rate was not a prerequisite for PHB accumulation, but a reduced or delayed accumulation of substrate appeared to enhance PHB accumulation. Under the best conditions, PHB constituted up to 63% of dry cell mass after 12?h of culture. The average biomass yield coefficient on sucrose was about 0.35, or a little less than in batch fermentations. The highest PHB concentrations attained were about 18?g?·?l^?1.     

Automated feeding strategies for high-cell-density fed-batch cultivation of Pseudomonas putida KT2440

Four automatic substrate feeding strategies were developed and investigated in this study to obtain rapid, repeatable, and reliable high cell densities of Pseudomonas putida KT2440 from glucose. Growth yield data of the key nutrients, Y _X/Glucose, Y _X/NH4, Y _X/PO4, Y _X/Mg, and Y _CO2/Glucose, were determined to be 0.41, 5.44, 13.70, 236, and 0.65 g g⁻¹, respectively. Although standard exponential feeding strategy worked well when the predetermined μ was set at 0.25 h⁻¹, an exponential glucose feeding strategy with online μ _max estimation resulted in a higher average biomass productivity (3.4 vs 2.8 g l⁻¹ h⁻¹). A CO₂ production rate based pulse glucose feeding strategy also resulted in good overall productivity (3.0 g l⁻¹ h⁻¹) and can be used as an alternative to pH-stat or DO-stat feeding. A cumulative CO₂ production based continuous feed with real-time cumulative glucose consumption estimation resulted in much higher biomass productivity (4.3 g l⁻¹ h⁻¹) and appears to be an excellent and reliable approach to fully automating high-cell-density fed-batch cultivation of P. putida.     

Competitive exclusion as a mode of action of a novel Bacillus cereus aquaculture biological agent

Aims: To determine the contribution of potential modes of action of a Bacillus cereus aquaculture biological control agent in inhibition of the fish pathogen, Aeromonas hydrophila. Methods and Results: When B. cereus was tested in plate well inhibition studies, no production of antimicrobial compounds was detected. Bacillus cereus had a high growth rate (0·96 h^?1), whereas Aer. hydrophila concentration decreased by c. 70% in co‐culture experiments. In nutrient limitation studies, B. cereus had a significantly higher growth rate when cultured under glucose (P < 0·05) and iron (P < 0·01) limitation in comparison with Aer. hydrophila. Bacillus cereus glucose (0·30 g l^?1 h^?1) and iron (0·60 mg l^?1 h^?1) uptake rates were also significantly higher (P < 0·01) than the Aer. hydrophila glucose (0·14 g l^?1 h^?1) and iron (0·43 mg l^?1 h^?1) uptake rates. Iron uptake was facilitated by siderophore production shown in time profile studies where relative siderophore production was c. 60% through the late exponential and sporulation phases. Conclusions: Competitive exclusion by higher growth rate, competition for organic carbon and iron, facilitated by siderophore production, could be identified as mechanisms of pathogen growth inhibition by B. cereus. Significance and Impact of the Study: This study is the first elucidation of the mechanism of action of our novel B. cereus biological agent in growth attenuation of pathogenic Aer. hydrophila. This study enhances the application knowledge and attractiveness for adoption of B. cereus NRRL 100132 for exploitation in aquaculture.     

Continuous production ofl-lactic acid from whey permeate by immobilizedLactobacillus casei subsp.casei

Summary The production of l-lactic acid from whey permeate, a waste product of the dairy industry, by fermentation with the lactic acid bacterium Lactobacillus casei subsp. casei was investigated. A fermentation medium consisting of permeate and supplements, which enables exponential growth of the organisms, was developed. A fast method for determination of free and immobilized biomass in solid-rich media, based on measurement of cellular ATP, was evolved. Continuous fermentations in a stirred tank reactor (STR) and in a fluidized bed reactor (FBR) with immobilized biomass were compared. In the STR a volumetric productivity of 5.5 g/l per hour at 100% substrate conversion [dilution rate (D) = 0.22 h^–1] was determined. In the FBR porous sintered glass beads were used for immobilization and a maximum biomass concentration of 105 g/kg support was measured. A productivity of 10 g/l per hour was obtained at D = 0.4 h^–1 (substrate conversion 93%) and of 13.5 g/l per hour at D = 1.0 h^–1 (substrate conversion 50%). Offprint requests to: W. Krischke     

Production of nisin Z using <Emphasis Type="Italic">Lactococcus lactis</Emphasis> IO-1 from hydrolyzed sago starch

A membrane bioreactor for production of nisin Z was constructed using Lactococcus lactis IO-1 in continuous culture using hydrolyzed sago starch as carbon source. A strategy used to enhance the productivity of nisin Z was to maintain the cells in a continuous growth at high cell concentration. This resulted in a volumetric productivity of nisin Z, as 50,000 IU l⁻¹ h⁻¹ using a cell concentration of 15 g l⁻¹, 30^°C, pH 5.5 and a dilution rate of 1.24 h⁻¹. Adding 10 g l⁻¹ YE and 2 g l⁻¹ polypeptone, other inducers were unnecessary to maintain production of nisin. The operating conditions of the reactor removed nisin and lactate, thus minimizing their effects which allowed the maintenance of cells in continuous exponential growth phase mode with high metabolic activity.     

Xylitol production from barley bran hydrolysates by continuous fermentation with Debaryomyces hansenii

The continuous bioconversion of xylose-containing solutions (obtained by acid hydrolysis of barley bran) into xylitol was carried out using the yeast Debaryomyces hansenii under microaerophilic conditions with or without cell recycle. In fermentations without cell recycle, the volumetric productivities ranged from 0.11–0.6 g l^–1 h^–1 were obtained for dilution rates of 0.008–0.088 h^–1. In experiments performed with cell recycle after membrane separation, the optimum xylitol productivity (2.53 g l^–1 h^–1) was reached at a dilution rate of 0.284 h^–1.     

Batch and continuous ribonuclease production by immobilized Aspergillus clavatus cells in a bubble-collumn bioreactor

Summary Ribonuclease production using immobilized cells (IC) of Aspergillus clavatus has been studied under batch, repeated-batch and continuous fermentation conditions in a bubble-column bioreactor and compared with production by free cells, Immobilization was achieved by the method of cryostructurization in polyvinyl alcohol beads. The effect of various aeration rates in a column bioreactor has been investigated. Enzyme production by IC [42 000 units (U)·l^–1] during batch fermentations was comparable to that of a free-cell system. The specific productivity of IC was 8.5 times higher than that of free cells. In repeated batch fermentation at various aeration rates, successful reuse of IC was obtained, with comparable levels of enzyme production. Continuous ribonuclease production was achieved for 44 days at 1 vvm aeration and a dilution rate of 0.0 h^–1 with volumetric productivity (450 U·1^–1) and yield.