Homo-fermentative production of d-lactic acid by Lactobacillus sp. employing casein whey permeate as a raw feed-stock

Casein whey permeate (CWP), a lactose-enriched dairy waste effluent, is a viable feed stock for the production of value-added products. Two lactic acid bacteria were cultivated in a synthetic casein whey permeate medium with or without pH control. Lactobacillus lactis ATCC 4797 produced d-lactic acid (DLA) at 12.5 g l^?1 in a bioreactor. The values of Leudking–Piret model parameters suggested that lactate was a growth-associated product. Batch fermentation was also performed employing CWP (35 g lactose l^?1) with casein hydrolysate as a nitrogen supplement in a bioreactor. After 40 h, L. lactis produced 24.3 g lactic acid l^?1 with an optical purity >98 %. Thus CWP may be regarded as a potential feed-stock for DLA production.     

Batch propagation of Lactobacillus helveticus for production of lactic acid from lactose concentrated cheese whey with microaeration and nutrient supplementation

Continuous mix batch bioreactors were used to study the kinetic parameters of lactic acid fermentation in microaerated-nutrient supplemented, lactose concentrated cheese whey using Lactobacillus helveticus. Four initial lactose concentrations ranging from 50 to 150 g l^–1 were first used with no microaeration and no yeast extract added to establish the substrate concentration above which inhibition will occur and then the effects of microaeration and yeast extract on the process kinetic parameters were investigated. The experiments were conducted under controlled pH (5.5) and temperature (42 °C) conditions. The results indicated that higher concentrations of lactose had an inhibitory effect as they increased the lag period and the fermentation time; and decreased the specific growth rate, the maximum cell number, the lactose utilization rate, and the lactic acid production rate. The maximum lactic acid conversion efficiency (75.8%) was achieved with the 75 g l^–1 initial lactose concentration. The optimum lactose concentration for lactic acid production was 75 g l^–1 although Lactobacillus helveticus appeared to tolerate up to 100 g l^–1 lactose concentration. Since the lactic acid productivity is of a minor importance compared to lactic acid concentration when considering the economic feasibility of lactic acid production from cheese whey using Lactobacillus helveticus, a lactose concentration of up to 100 g l^–1 is recommended. Using yeast extract and/or microaeration increased the cell number, specific growth rate, cell yield, lactose consumption, lactic acid utilization rate, lactic acid concentration and lactic acid yield; and reduced the lag period, fermentation time and residual lactose. Combined yeast extract and microaeration produced better results than each one alone. From the results it appears that the energy uncoupling of anabolism and catabolism is the major bottleneck of the process. Besides lactic acid production, lactose may also be hydrolysed into glucose and galactose. The -galactosidase activity in the medium is caused by cell lysis during the exponential growth phase. The metabolic activities of Lactobacillus helveticus in the presence of these three sugars need further investigation.     

Culture conditions of tannase production by Lactobacillus plantarum

Lactobacillus plantarum produced an extracellular tannase after 24 h growth on minimal medium of amino acids containing 2 g tannic acid l^–1. Enzyme production (6 U ml^–1) was optimal at 37 °C and pH 6 with 2 g glucose l^–1 and 7 g tannic acid l^–1 in absence of O₂.     

Acetic acid production from whey lactose by the co-culture ofStreptococcus lactis andClostridium formicoaceticum

Summary Acetic acid was produced from anaerobic fermentation of lactose by the co-culture ofStreptococcus lactis andClostridium formicoaceticum at 35° C and pHs between 7.0 and 7.6. Lactose was converted to lactic acid, and then to acetic acid in this mixed culture fermentation. The overall acetic acid yield from lactose was about 95% at pH 7.6 and 90% at pH 7.0. The fermentation rate was also higher at pH 7.6 than at pH 7.0. In batch fermentation of whey permeate containing about 5% lactose at pH 7.6, the concentration of acetic acid reached 20 g/l within 20 h. The production rate then became very slow due to end-product inhibition and high Na⁺ concentration. About 30 g/l acetate and 20 g/l lactate were obtained at a fermentation time of 80 h. However, when diluted whey permeate containing 2.5% lactose was used, all the whey lactose was converted to acetic acid within 30 h by this mixed culture.     

Sophorolipid Production with High Yields on Whey Concentrate and Rapeseed Oil without Consumption of Lactose

Sophorolipids were produced by single-step batch cultivation of Candida bombicola ATCC 22214 on deproteinized whey concentrate and repeated feed of rapeseed oil. A mild sterilization method for whey was developed. High yields of 280 g dry sophorolipids l^–1 were obtained from deproteinized whey concentrate containing 100 g lactose l^–1 and 300 g rapeseed oil l^–1. Surprisingly, the whey lactose was not consumed by the organism. Growth only on the oil was assumed and a high lipase activity of 24 U per g cell dry weight resulted.     

Embryogenic protoplast cultures of orange jessamine (Murraya paniculata) and their regeneration into plants flowering in vitro

Embryogenic callus was induced from the hypocotyl region of seedlings germinated from immature embryos of orange jessamine (Murraya paniculata (L.) Jack) on Murashige & Tucker (1969) medium containing 50 g l^-1 sucrose, 5.0 mg l^-1 benzyladenine, 2.5 mg l^-1 2,4-dichlorophenoxyacetic acid and 600 mg l^-1 malt extract. Isolated protoplasts divided to produce callus on Murashige & Tucker (1969) medium containing 50 g l^-1 sucrose, 0.01 mg l^-1 gibberellin A₄₊₇ and 600 mg l^-1 malt extract. Callus developed to plantlets via somatic embryogenesis on Murashige & Tucker (1969) medium with 50 g l^-1 lactose but no plant growth regulators. These plantlets flowered in vitro on half strength Murashige & Tucker (1969) medium containing 50 g l^-1 sucrose after 2 months culture.Abbreviations BA benzyladenine - 2,4-d 2,4-dichlorophenoxyacetic acid - FDA fluorescein diacetate - FM full strength MT medium - FMG full strength MT medium +1 mg l^-1 GA₃ - GA₃ gibberellin A₃ - GA₄₊₇ gibberellin A₄₊₇ - HM half strength MT medium - HMG half strength MT medium +1 mg l^-1 GA₃ - MT Murashige & Tucker (1969)     

Optimization of cell growth and poly(glutamic acid) production in batch fermentation by Bacillus subtilis

Poly(glutamic acid) was produced maximally by Bacillus subtilis in batch fermentations at pH 7 and using glycerol at 20 g l^–1 in a glutamic acid/citric acid medium. Poly(glutamic acid) reached 23 g l^–1 after 30 h.     

Synbiotic Fermentation for the Co‐Production of Lactic and Lactobionic Acids from Residual Dairy Whey

Besides its properties as an antioxidant, stabilizer, or acidifier, lactobionic acid has emerged as a potential prebiotic compound, raising the possibility of being included together with the probiotic microorganism Lactobacillus casei in novel functional fermented foods with synbiotic characteristics. Their manufacturing strategy could benefit from the recently implemented microbial synthesis of lactobionic acid by the strong producer Pseudomonas taetrolens, employing residual dairy whey as raw material. The phenomenon of amensalism established between Pseudomonas and Lactobacillus makes simultaneous fermentation unfeasible. A novel sequential process has been developed in which L. casei is inoculated in a second step. Its ability to utilize lactobionic acid as a carbon and energy source was previously tested. Experimental results showed the capacity of L. casei to work efficiently on the residual substrate fermented by P. taetrolens, producing lactic acid by degrading the remaining lactose, with a lactic acid yield on substrate and productivity of 0.95 g g^?1 and 0.20 g L^?1 h^?1, respectively. Lactobionic acid was barely consumed in this complex growth medium, thus ensuring its presence in the resulting fermented product. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:1250–1256, 2017     

Propionic acid fermentation of ultra-high-temperature sterilized whey using mono-and mixed-cultures

Summary Unlike sterilization by autoclave (Anderson et al. 1986) high concentrations of cheese whey sterilized by ultra high temperature (UHT) resulted in a medium conducive to microbial growth and propionic acid production. Propionibacterium freudenreichii ss. shermanii, grown with pH control in 12% whey solids and 1% yeast extract sterilized by UHT, produced about 1.9% propionic acid within 70 h; more than 50% of the lactose was not used. Under similar conditions, mixed cultures of P. shermanii and Lactobacillus casei produced more than 3.0% propionic acid. Acclimating the mixed culture to the whey medium resulted in 4.5% propionic acid. The amount of propionic acid produced was further increased to about 6.5% by raising the concentration of whey solids to about 18%. Using the mixed culture, all the lactose was consumed and lactic acid did not accumulate.     

Influence of pH,lactose and lactic acid on the growth of Streptococcus cremoris: a kinetic study

Summary The effect of various culture conditions on growth kinetics of an homofermentative strain of the lactic acid bacterium Streptococcus cremoris were investigated in batch cultures, in order to facilitate the production of this organism as a starter culture for the dairy industry. An optimal pH range of 6.3–6.9 was found and a lactose concentration of 37 g·l^-1 was shown to be sufficient to cover the energetic demand for biomass formation, using the recommended medium. The study of the effect of lactic acid concentration on growth kinetics revealed that the end-product was not the sole factor affecting growth. The strain was characterized for its tolerance towards lactic acid and a critical concentration of 70 g·l^-1 demonstrated. With the product yield of 0.9 g·g^-1 at non-lactose limiting conditions the lactic acid concentration of 33 g·l^-1 could not explain the low growth rates obtained, implicating a nutritional limitation.Symbols t _f fermentation duration (h) - X Biomass concentration (g·l^-1) - X _m maximum biomass concentration (g·l^-1) - S lactose concentration (g·l^-1) - S _r residual lactose concentration (g·l^-1) - P produced lactic acid concentration (g·l^-1) - P _a added lactic acid concentration (g·l^-1) - P _c critical lactic acid concentration (g·l^-1) - specific growth rate (h^-1) - _max maximum specific growth rate (h^-1) - R _x/S biomass yield (g·g^-1) calculated when =0 - R _P/S product yield (g·g^-1)     

Protein production from whey usingPenicillium cyclopium; growth parameters and cellular composition

Summary The growth parameters ofPenicillium cyclopium have been evaluated in a continuous culture system for the production of fungal protein from whey. Dilution rates varied from 0.05 to 0.20 h^–1 under constant conditions of temperature (28°C) and pH (3.5). The saturation coefficients in the Monod equation were 0.74 g l^–1 for lactose and 0.14 mg l^–1 for oxygen, respectively. For a wide range of dilution rates, the yield was 0.68 g g^–1 biomass per lactose and the maintenance coefficient 0.005 g g^–1 h^–1 lactose per biomass, respectively. The maximum biomass productivity achieved was 2 g l^–1 h^–1 biomass at dilution rates of 0.16–0.17 h^–1 with a lactose concentration of 20 g l^–1 in the feed. The crude protein and total nucleic acid contents increased with a dilution rate, crude protein content varied from 43% to 54% and total nucleic acids from 6 to 9% in the range of dilution rates from 0.05 to 0.2 h^–1, while the Lowry protein content was almost constant at approximately 37.5% of dry matter.Nomenclature (mg l^–1) C_o initial concentration of dissolved oxygen - (h^–1) D dilution rate - (mg l^–1) K₀₂ saturation coefficient for oxygen - (g l^–1) K_s saturation coefficient for substrate - (g g^–1 h^–1) lactose per biomass) m maintenance energy coefficient - (mM g^–1 h^–1O₂ per biomass) Q₀₂ specific oxygen uptake rate - (g l^–1) S residual substrate concentration at steady state - (g l^–1) S_o initial substrate concentration in feed - (min) t_1/2 time when C_o is equal to C_o/2 - (g l^–1) X biomass concentration - (g l^–1) X biomass concentration at steady state - (g g^–1 biomass per lactose) Y_G yield coefficient for cell growth - (g g^–1 biomass per lactose) Y_x/s overall yield coefficient - (h^–1) specific growth rate     

Poly-(3-hydroxybutyrate) production from whey by high-density cultivation of recombinant Escherichia coli

Recombinant Escherichia coli strain GCSC 6576, harboring a high-copy-number plasmid containing the Ralstonia eutropha genes for polyhydroxyalkanoate (PHA) synthesis and the E. coli ftsZ gene, was employed to produce poly-(3-hydroxybutyrate) (PHB) from whey. pH-stat fed-batch fermentation, using whey powder as the nutrient feed, produced cellular dry weight and PHB concentrations of 109 g l⁻¹ and 50 g l⁻¹ respectively in 47 h. When concentrated whey solution containing 210 g l⁻¹ lactose was used as the nutrient feed, cellular dry weight and PHB concentrations of 87 g l⁻¹ and 69 g l⁻¹ respectively could be obtained in 49 h by pH-stat fed-batch culture. The PHB content was as high as 80% of the cellular dry weight. These results suggest that cost-effective production of PHB is possible by fed-batch culture of recombinant E. coli using concentrated whey solution as a substrate. Received: 19 December 1997 / Received revision: 17 March 1998 / Accepted: 20 March 1998     

Effect of medium acidity on growth and rooting of different plant species growing in vitro

Micropropagated Choisya, Daphne, Delphinium, Hemerocallis, Hosta, Iris and Photinia were found to adjust the pH of Murashige and Skoog's plant tissue culture medium (initial pH 5.6 or 3.5) to different values depending on the species. When plant growth and rooting rates were determined after plants had been grown on media initially adjusted or buffered to values between 2.6 and 5.7 the different plant species were also found to have distinct pH requirements for optimal growth and/or rooting rates.Abbreviations MS Murashige & Skoog's (1962) medium - MS19 MS with additionally 10 g l^–1 sucrose - 80 mg l^–1 adenine sulphate and 130.9 mg l^–1 NaH₂PO₄ - BA 6-benzyladenine - NAA 1-naphthyl-acetic acid - IBA 3-indole-butyric acid - IAA 3-indole-acetic acid - 2iP N₆(2-isopentyl) adenine     

Effect of phenoxyalkanoic acid herbicides on the fermentative production of l-lysine

Summary The effect of the herbicides MCPA, MCPB, mecoprop, dichlorprop, 2,4-D, 2,4-DB, and 2,4,5-T on l-lysine fermentation was investigated using a lysine-producing mutant of Corynebacterium glutamicum. Stimulation of l-lysine production by 6% to 36% was observed in shaken flask experiments when the test herbicides were added at a concentration of 5 · 10^-4 M to growing cultures after 24 h of cultivation. The most effective stimulators were MCPA, mecoprop and dichlorprop.Detailed studies of the effect of MCPA (5 · 10^-6 M to 5 · 10^-3 M) showed that the degree of stimulation depended on medium composition and aeration. In the synthetic medium, maximum production of 50 g · l^-1 lys · HCl occurred at 5 · 10^-4 M MCPA and an oxygen transfer rate (OTR) of 1.97 g O₂ · l^-1 · h^-1, while 61.7 g · l^-1 of lys · HCL was formed at 5 · 10^-3 M MCPA and an OTR of 3.75 g O₂ · l^-1 · h^-1. In the amino-nitrogen rich medium, maximum production of 42 g · l^-1 lys · HCl was observed at 5 · 10^-6 M MCPA and an oxygen transfer rate of 1.5 g O₂ · l^-1 · h^-1. Results from batch l-lysine fermentation in a fermenter showed similar stimulatory effects, with an optimal concentration of MCPA for l-lysine production of 5 · 10^-5 M. Without herbicide addition, the test strain produced 16.25 g · l^-1 of product and with addition of 5 · 10^-5 M MCPA, the same strain produced 52.1 g · l^-1 lys · HCl after 72 h of fermentation.Abbreviations MCPA 2-methyl-4-chlorophenoxyacetic acid - MCPB 2-methyl-4-chlorophenoxybutyric acid - mecoprop 2-methyl-4-chlorophenoxypropionic acid - dichlorprop 2,4-dichlorophenoxypropionic acid - 2,4-D 2,4-dichlorophenoxyacetic acid - 2,4-DB 2,4-dichlorophenoxybutyric acid - 2,4,5-T 2,4,5-trichlorophenoxyacetic acid     

Influence of temperature rise on kinetic parameters during batch propagation of Kluyveromyces fragilis in cheese whey under ambient conditions

Three 5 l working volume fermenters were used to investigate the growth of the yeast Kluyveromyces fragilis in acid cheese whey under ambient temperature in order to assess the specific growth rate and yield, the lactose and oxygen uptake rates during the various phases of batch culture, the effect of increasing temperature on the various kinetic parameters, and the need for a cooling unit for single cell production batch systems. The initial dissolved oxygen in the medium was 5.5 mg l^–1 and the pH was maintained at 4.5. The observed lag phase, specific growth rate and maximum cell number were 4 h, 0.2 h^–1 and 8.4 × 10⁸ cells ml^–1, respectively. About 99% of the lactose in cheese whey was utilized within 20 h, 85% during the exponential growth phase. The specific lactose utilization rates by K. fragilis were 0.20 × 10^–12, 1.457 × 10^–12, 0.286 × 10^–12 and 0.00 g lactose cell^–1 h^–1, for the lag, exponential, stationary and death phases, respectively. The dissolved oxygen concentration in the medium decreased as the cell number increased. The lowest oxygen concentration of 1.2 mg l^–1 was observed during the stationary phase. The volumetric oxygen transfer coefficient was 0.41 h^–1 and the specific oxygen uptake rates were 0.32 × 10^–12, 2.14 × 10^–12, 0.51 × 10^–12 and 0.003 × 10^–12 mg O₂ cell^–1 h^–1, for the lag, exponential, stationary and death phases, respectively. The maximum temperature recorded for the medium was 33 °C, indicating that a cooling unit for batch production of single cell protein at ambient temperature is not needed for this type of bioreactor. The increase in medium temperature affected the cell growth and the lactose and oxygen uptake rates.     

Simulation of fermentation conditions for vitamin B12 biosynthesis from whey

Vitamin B₁₂ production in fermentation of Propionibacterium shermanii and Propionibacterium arl AKU 1251 in whey permeate medium has been studied. The observed results and simulated expected values obtained by fitting statistical equations to the recorded data showed that 24 h old inoculum, 5 mg iron l^?1 and 4% whey lactose were optimal for vitamin B₁₂ biosynthesis in both strains when fermentation was carried out under anerobic (84 h) and aerobic (84 h) conditions at 30°C. The supplementation of whey medium with 0.5% (NH₄)₂HPO₄ enhanced further the metabolite yield; however, the preference for a mixed carbon source (lactose + d-glucose or lactose + d-fructose) at different levels varied in the strains under study. P. shermanii, under optimal cultural conditions, was found to be a better strain than Propionibacterium arl AKU, 1251 in fermenting whey lactose for product (vitamin B₁₂) formation.     

Lactosucrose production by various microorganisms harboring levansucrase activity

Production of the artificial sweetener, lactosucrose, by various microorganisms containing levansucrase activity was investigated. Of the tested bacteria, Bacillus subtilis was the most effective producer using lactose as an acceptor and sucrose as a fructosyl donor. Lactosucrose production by this strain was optimal at pH 6.0 and 55 °C whereupon 181 g lactosucrose l^–1 was produced from 225 g lactose l^–1 and 225 g sucrose l^–1 in 10 h.     

Metabolic engineering for direct lactose utilization by Saccharomyces cerevisiae

A recombinant strain of Saccharomyces cerevisiae, secreting -galactosidase from Kluyveromyces lactis, grew efficiently with more than 60 g lactose l^–1. The growth rate (0.23 h^–1) in a cheese-whey medium was close to the highest reported hitherto for other recombinant S. cerevisiae strains that express intracellular -galactosidase and lactose-permease genes. The conditions for growth and -galactosidase secretion in this medium were optimized in a series of factorial experiments. Best results were obtained at 23 °C for 72 h. Since the recombinant strain produced less than 3% ethanol from the lactose, it was also assayed for the production of fructose 1,6-bisphosphate from cheese whey, and 0.06 g l^–1 h^–1 were obtained.     

Ethanol production from whey permeate by immobilized yeast cells

The ability of two yeast strains to utilize the lactose in whey permeate has been studied. Kluyveromyces marxianus NCYC 179 completely utilized the lactose (9.8%), whereas Saccharomyces cerevisiae NCYC 240 displayed an inability to metabolize whey lactose for ethanol production. Of the two gel matrices tested for immobilizing K. marxianus NCYC 179 cells, sodium alginate at 2% (w/v) concentration proved to be the optimum gel for entrapping the yeast cells effectively. The data on optimization of physiological conditions of fermentation (temperature, pH, ethanol concentration and substrate concentration) showed similar effects on immobilized and free cell suspensions of K. marxianus NCYC 179, in batch fermentation. A maximum yield of 42.6 g ethanol l^?1 (82% of theoretical) was obtained from 98 g lactose l^?1 when fermentation was carried at pH 5.5 and 30°C using 120 g dry weight l^?1 cell load of yeast cells. These results suggest that whey lactose can be metabolized effectively for ethanol production using immobilized K. marxianus NCYC 179 cells.     

Control of ethanol production and monitoring of membrane performance by mass-spectrometric gas analysis in the coupled fermentation-pervaporation of whey permeate

A coupled fermentation-pervaporation process was operated continuously with on-line mass spectrometric gas analysis monitoring of product accumulation on both the upstream and the downstream sides of the membrane. Efficient coupling of the fermentation with pervaporation was attained when a steady state of ethanol production and removal was achieved with whey permeate containing high concentrations of lactose (>8%) or by controlled lactose additions that also compensated for loss of liquid due to pervaporation. The combined system consists of a tubular membrane pervaporation module, directly connected to a stirred fermentor to form one circulation loop, kept at 38°C, with both units operating under computer control. Mass spectrometric gas analysis of the CO₂ gas evolved in the fermentor and the ethanol and water in the pervaporate on the downstream side of the membrane enabled us to follow the production of ethanol and its simultaneous removal. Membrane selectivity was calculated on-line and served to monitor the functioning of the membrane. Batch-wise-operated fermentation-pervaporation with Candida pseudotropicalis IP-513 yielded over 120 gl^–1 of concentrated ethanol solution using supplemented whey permeate containing 16% lactose. A steady state lasting for about 20 h was achieved with ethanol productivity of 20 g h^–1 (approx. 4 g l^–1 h^–1). Membrane selectivity was over 8. Controlled feeding of concentrated lactose suspension in the whey permeate (350 g l^–1) resulted in the continuous collection of 120–140 g l^–1 of ethanol pervaporate for 5 days, by which time salt accumulation hampered the fermentation. Medium refreshment restored the fermentative activity of the yeast cells and further extended the coupled process to over 9 days (200 h), when reversible membrane fouling occurred. The membrane module was exchanged and the combined process restarted. Correspondence to: Y. Shabtai