Biodegradation of phenol using the self-cycling fermentation (SCF) process

Self-cycling fermentation (SCF) in a stirred tank reactor was applied to the biodegradation of phenol by Pseudomonas putida. The technique resulted in stable and repeatable performance. Complete substrate consumption was achieved under all operating conditions investigated. SCF resulted in substrate utilization rates as high as 14.5 kg of phenol per cubic meter of fermentor volume per day of fermentation, higher than those that have been reported for batch, CSTR, and packed column fermentors. A mathematical model of the self-cycling fermentation process was expanded to include inhibitory substrate-microorganism combinations, and was shown to provide a good fit to both end-of-cycle and intracycle experimental data. (c) 1996 John Wiley & Sons, Inc.     

Application of self-cycling fermentation technique to the production of poly-beta-hydroxybutyrate

The production of poly-beta-hydroxybutyrate (PHB) by Alcaligenes eutrophus DSM 545 in a cyclone bioreactor was compared using various culture methods: batch, fed-batch, and self-cycling fermentation (SCF) with and without extended periods of nutrient deprivation. SCF is a semi-continuous method that results in a nutrient limitation for every successive generation of cells and, therefore, may have advantages for products whose formation follow secondary metabolite kinetics. Use of the SCF technique without extended nutrient deprivation produced a PHB concentration of 1.2 g L(-1) as 40% of the biomass dry weight. With nitrogen deprivation for 4 or 6 h, the concentration of PHB decreased when compared to the standard SCF technique. However, nitrogen deprivation periods of 8 h resulted in an increase in PHB concentration to 2.7 g L(-1) or 59% of the biomass dry weight. The nutrient cycling may act to repress PHB accumulation during periods of nitrogen deprivation, unless a time threshold has been reached, after which PHB accumulation occurs as in normal batch culture. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 815-820, 1997.     

Two-stage fermentation process for the production of calcium magnesium acetate and propionate road deicers

Calcium magnesium acetate (CMA) and propionate (CMP) are environmentally benign deicing chemicals that can replace sodium chloride that is widely used on roads and highways at present for snow and ice control to provide safe driving conditions during winter. The price of CMA from petroleum-derived acetic acid is quite expensive. Anaerobic fermentations have not proven economical due to the low acid productivity and concentrations. A novel method for the production of CMA and CMP from lactose and whey permeate via a two-stage anoxic fermentation system, with calcium hydroxide for pH control is described in this paper. A homolactic bacterium Lactobacillus plantarum is used to convert lactose to calcium magnesium lactate (CML) in the first stage, and Propionicibacterium acidipropionici P200910 is used to convert CML to CMA and CMP in the second stage. In both stages, the conversion rates were 90% (w/w). Lactic acid productivity was 2.03 g/L/h in the first stage at a dilution ratio of 0.06 h⁻¹. Propionic and acetic acid yield was 1.79 g/L/h at a dilution rate of 0.05 h⁻¹. Calcium hydroxide addition did not significantly alter the overall yield of acids in either stage. However, the ratio of concentration of propionate to acetate in the final product changed from 3.0 when NaOH is used to 2.0 when lime is applied for pH control. After separation of the biomass, the liquid with a total concentration of 48–55 g/L of CMA and CMP can be processed to obtain a solid road deicer product.     

Two-stage continuous process development for the production of medium-chain-length poly(3-hydroxyalkanoates)

Pseudomonas oleovorans forms medium-chain-length poly(3-hydroxyalkanoate) (PHA) most effectively at growth rates below the maximum specific growth rate. Under adequate conditions, PHA accumulates in inclusion bodies in cells up to levels higher than half of the cell mass, which is a time-consuming process. For PHA production, a two-stage continuous cultivation system with two fermentors connected in series is a potentially useful system. It offers production of cells at a specific growth rate in a first compartment at conditions that lead cells to generate PHA at higher rates in a second compartment, with a relatively long residence time. In such a system, dilution rates of 0.21 h(-1) in the first fermentor (D(1)) and 0.16 h(-1) in the second fermentor (D(2)) were found to yield the highest volumetric PHA productivity. Transient-state experiments allowed investigation of D(1) and D(2) over a wide dilution rate range at high resolution in time-saving experiments. Furthermore, the influence of temperature, pH, nutrient limitation, and carbon source on PHA productivity was investigated and results similar to optimum conditions in single-stage chemostat cultivations of P. oleovorans were found. With all culture parameters optimized, a volumetric PHA productivity of 1.06 g L(-1) h(-1) was determined. Under these conditions, P. oleovorans cells contained 63% (dry weight) PHA in the effluent of the second fermentor. This is the highest PHA productivity and PHA content reported thus far for P. oleovorans cultures grown on alkanes.     

Antibiotic production by Streptomyces aureofaciens using self-cycling fermentation

The self-cycling frementation (;rSCF) technique was applied to culture of Streptomyces aureofaciens. SCF is a method of continuous fermentation in which the metabolism of a microorganism is monitored by a measurement such as dissolved oxygen. These data are sent to a computer to allow it to control the system. Tetracycline production was observed only at exceedingly low iron concentrations in the growth medium. Repeatability of cycles was found to be dependent upon the presence of tetracycline in the fermentation broth as well as the strain of microorganism grown in the fermentor. Tetracycline was produced by an improved specific rate when compared to results in the literature for this organism grown using the batch method. (c) 1994 John Wiley & Sons, Inc.     

Two-stage fermentation process for enhanced mannitol production using Candida magnoliae mutant R9

Mutants of Candida magnoliae NCIM 3470 were generated by treatment of ultra-violet radiations, ethyl methyl sulphonate and N-methyl-N′-nitro-N-nitrosoguanidine. Mutants with higher reductase activity were screened by means of 2,3,5-triphenyl tetrazolium chloride agar plate assay. Among the screened mutants, the mutant R9 produced maximum mannitol (i.e. 46 g l^?1) in liquid fermentation medium containing 250 g l^?1 glucose and hence was selected for further experiments. Preliminary optimization studies were carried out on shake-flask level which increased the mannitol production to 60 g l^?1 in liquid fermentation medium containing 300 g l^?1 glucose. A two-stage fermentation process comprising of growth phase and production phase was employed. During the growth phase, glucose was supplemented and aerobic conditions were maintained. Thereafter, the production phase was initiated by supplementing fructose and switching to anaerobic conditions by discontinuing aeration and decreasing the speed of agitation. The strategy of two-stage fermentation significantly enhanced the production of mannitol up to 240 g l^?1, which is the highest among all fermentative production processes and corresponds to 81 % yield and 4 g l^?1 h^?1 productivity without formation of any by-product.     

Two-stage batch process for the production of ajmalicine by Catharanthus roseus: The link between growth and production stage

The link between the growth stage and the production stage in a two-stage batch process was investigated using (filtered) inocula from different periods of the stationary phase of the growth cycle. In the production stage, ajmalicine production by Catharanthus roseus in a 3-L stirred tank reactor was induced with a high glucose concentration (80 g/L). Ajmalicine production in cultures started with cells from the late stationary phase was five times higher than in cultures started with cells from the early stationary phase. After transfer to the production stage, cells from the early stationary phase showed a transient increase in respiration and enzyme induction, followed by culture browning. In contrast, cells in the late stationary phase showed a typical induction pattern: constant respiration, and permanent enzyme induction. A striking similarity between the geraniol-10-hydroxylase (G10H) activity and the ajmalicine accumulation profile could be observed in all cultures, suggesting that G 10H regulated ajmalicine production in this investigation. The intracellular nitrate concentration was significantly higher in the inoculum showing a high ajmalicine production than in the inoculum with a low production. Consequently, nitrate may act as a marker for the start of the production stage: as soon as the nitrate is depleted in the growth medium secondary metabolism can be induced. (c) 1995 John Wiley & Sons, Inc.     

Two-stage maturation process for newly replicated chromatin

HTC cells have been labeled by short exposures to [3H]thymidine in order to identify newly synthesized DNA. By either isolating nuclei directly or isolating them after an extensive fixation with formaldehyde, we have been able to identify two phases in the maturation process of newly replicated chromatin. The first phase which is relatively brief (less than 5 min) is reflected in a diffuse, irregular organization of nucleosomes on new DNA immediately postreplicatively . The second phase which lasts from 5 to 30 min postreplication is characterized by a normal repeat length for the nucleosomes which are nonetheless more weakly bound than bulk nucleosomes. This is reflected in increased sliding during nuclease digestion as well as increased nuclease sensitivity and the presence of easily dissociated histones which has been described by other workers.     

Mathematical model of self-cycling fermentation

This article presents a mathematical model for biomass, limiting substrate, and dissolved oxygen concentrations during stable operation of self-cycling fermentation (SCF). Laboratory experiments using the bacterium Acinetobacter calcoaceticus RAG-1 and ethanol as the limiting substrate were performed to validate the model. A computer simulation developed from the model successfully matched experimental SCF intracycle trends and end-of-cycle results and, most importantly, settled into an unimposed periodicity characteristic of stable SCF operation. (c) 1995 John Wiley & Sons, Inc.     

Two-stage optimization process for formulation of chitosan microspheres

The objective of the present study was to optimize the concentration of a chitosan solution, stirring speed, and concentration of drugs having different aqueous solubility for the formulation of chitosan microspheres. Chitosan microspheres (unloaded and drug loaded) were prepared by the chemical denaturation method and were subjected to measurement of morphology, mean particle size, particle size distribution, percentage drug entrapment (PDE), drug loading, and drug release (in vitro). Morphology of the microspheres was dependent on the level of independent process parameters. While mean particle size of unloaded microspheres was found to undergo significant change with each increase in concentration of chitosan solution, the stirring rate was found to have a significant effect only at the lower level (ie, 2000 to 3000 rpm). Of importance, spherical unloaded microspheres were also obtained with a chitosan solution of concentration less than 1 mg/mL. Segregated unloaded microspheres with particle size in the range of 7 to 15 microm and mean particle size of 12.68 microm were obtained in the batch prepared by using a chitosan solution of 2 mg/mL concentration and stirring speed of 3000 rpm. The highest drug load ( microg drug/mg microspheres) was 50.63 and 13.84 for microspheres containing 5-fluorouracil and methotrexate, respectively. While the release of 5-fluorouracil followed Higuchi's square-root model, methotrexate released more slowly with a combination of first-order kinetics and Higuchi's square-root model. The formation of chitosan microspheres is helped by the use of differential stirring. While an increase in the concentration of water-soluble drug may help to increase PDE and drug load over a large concentration range, the effect is limited in case of water-insoluble drugs.     

Two-stage cultures for the production of astaxanthin from Haematococcus pluvialis

A two-stage culture system was established for the production of astaxanthin from Haematococcus pluvialis. In a first stage green vegetative cells were produced in semicontinuous cultures maintained with daily renewal rates between 10 and 40%. The steady-state cell density decreased with increasing renewal rates. Highest cell productivity, 64 x 10(6) cells l(-1) day(-1) was obtained with a daily renewal rate of 20%. In a second stage the harvested cultures were submitted to high light (240 micromol photon m(-2) s(-1)) under batch conditions for 15 days in order to stimulate the transition to the aplanospore stage and the accumulation of astaxanthin. No decrease in cell density was recorded during the induction period in any of the cultures. Cultures obtained at high renewal rates continued growing during the induction period and no astaxanthin was accumulated until all nitrogen in the media had been consumed. The final concentration of astaxanthin was inversely correlated to the growth rate at which first-stage cultures were maintained. Optimal renewal rate for maximal astaxanthin production depended on the duration of the induction period. After a 12-day induction period the highest astaxanthin production, 5.8 mg l(-1) of semi-continuous culture day -1, was obtained with cultures maintained at a renewal rate of 20%. When the induction period was increased to 15 days maximal astaxanthin productivity, 9.6 mg l(-1) of semi-continuous culture day -1, was obtained from cultures maintained at a renewal rate of 40% despite the much lower astaxanthin concentration achieved in these cultures. Results demonstrate the feasibility of semi-continuous cultivation of H. pluvialis for the two-stage production of astaxanthin.     

Two-stage culture process for improved production of ganoderic acid by liquid fermentation of higher fungus Ganoderma lucidum

Investigations on the impact of pellet size on the cellular oxygen uptake and accumulation of ganoderic acid (GA) suggested the favorable effect of oxygen limitation on GA formation by the higher fungus Ganoderma lucidum. A two-stage fermentation process was thus proposed for enhanced GA production by combining conventional shake-flask fermentation with static culture. A high cell density of 20.9 g of DW/L (DW = dry cell weight) was achieved through a 4-day shake-flask fermentation followed by a 12-day static culture. A change in the cell morphology and a decrease in the sugar consumption rate were observed during the static culture. The GA production in the new two-stage process was considerably enhanced with its content increased from 1.36 (control) to 3.19 mg/100 mg of DW, which was much higher than previously observed.     

Two-stage fermentation method for production of protein-enriched feed from cassava

Studies have been carried out into the production of microbial protein from cassava using Trichoderma reesei and yeast. In monoculture studies, T. reesei was grown on whole cassava medium to give 0.74g dry cell/g cassava. The dry material contained 42% protein. The culture filtrate contained 5.8 g/l glucose, which supported the growth of yeast. Mixed culture fermentation was also carried out with the two microorganisms. Besides accelerating the rate of degradation and conversion of cassava to cells (0.85g cell/g cassava) the yeast boosted the protein content of the growth product to 51%.     

Two-stage biohumus production from inedible potato biomass

The feasibility of a two-stage bioconversion of inedible potato biomass into biohumus by oyster mushroom followed by worms was tested. As a raw material for biohumus production the inedible potato biomass in certain properties ranked below wheat straw. The most feasible method to convert the potato wastes into biohumus was to mix them with wheat straw at the mass ratio of 1:3 and then treat with mushrooms followed by worms. This gave a good yield of mushrooms. The biohumus produced from the mixture was suitable for use as a plant growth medium.     

Two-stage fermentation process for alginate production by Azotobacter vinelandii mutant altered in poly-β-hydroxybutyrate (PHB) synthesis

Aims:  A two-stage fermentation strategy, based on batch cultures conducted first under non-oxygen-limited conditions, and later under oxygen-limited conditions, was used to improve alginate production by Azotobacter vinelandii (AT6), a strain impaired in poly-β-hydroxybutyrate (PHB) production.
Methods and Results:  The use of sucrose as carbon source, as well as a high oxygen concentration (10%), allowed to obtain a maximum biomass concentration of 7·5 g l⁻¹ in the first stage of cultivation. In the second stage, the cultures were limited by oxygen (oxygen close to 0%) and fed with a sucrose solution at high concentration. Under those conditions, the growth rate decreased considerably and the cells used the carbon source mainly for alginate biosynthesis, obtaining a maximum concentration of 9·5 g l⁻¹, after 50 h of cultivation.
Conclusion:  Alginate concentration obtained from the AT6 strain was two times higher than that obtained using the wild-type strain (ATCC 9046) and was the highest reported in the literature. However, the mean molecular mass of the alginate produced in the second stage of the process by the mutant AT6 was lower (400 kDa) than the polymer molecular mass obtained from the cultures developed with the parental strain (950 kDa).
Significance and Impact of the Study:  The use of a mutant of A. vinelandii impaired in the PHB production in combination with a two-stage fermentation process could be a feasible strategy for the production of alginate at industrial level.     

Ability of acceptance for bacteriophages during verotoxin production by bacilli of the Enterobacteriaceae family]

Lysogenised verotoxigenic strains are the source of structural genes of verocytotoxins (stx-1 and stx-2) for the others intestinal bacili. The aim of the study was to estimate the ability of transfer of bacteriophages induced with UV irradiation from reference verotoxigenic strains of E. coli O157:H7 (CB571 and EDL933) into 125 wild-strains of bacili of Enterobacteriaceae family. None of tested recipient strains showed the production of cytotoxin on Vero and HeLa cell lines, what was acknowledged as the lack of six genes. Contrary to the laboratory strain of E. coli C600 none of 125 tested recipient strains accepted the phages. Obtained lysogenised laboratory strains of E. coli C600/CB571 and E. coli C600/EDL933, besides of the ability to produce verotoxins (with the presence of stx-1 and stx-2 genes), did not differ phenotypically and genotypically from parent strain of E. coli C600. The estimation of the ability to transfer of phages carried stx-1 and/or stx-2 genes was impossible because of too small number of tested wild strain of bacili or because of really low frequency of acceptation of phages by wild strains of intestinal bacili.     

Two-stage heterotrophic and phototrophic culture strategy for algal biomass and lipid production

A two-stage heterotrophic and phototrophic culture strategy for algal biomass and lipid production was studied, wherein high density heterotrophic cultures of Chlorellasorokiniana serve as seed for subsequent phototrophic growth. The data showed growth rate, cell density and productivity of heterotrophic C.sorokiniana were 3.0, 3.3 and 7.4 times higher than phototrophic counterpart, respectively. Hetero- and phototrophic algal seeds had similar biomass/lipid production and fatty acid profile when inoculated into phototrophic culture system. To expand the application, food waste and wastewater were tested as feedstock for heterotrophic growth, and supported cell growth successfully. These results demonstrated the advantages of using heterotrophic algae cells as seeds for open algae culture system. Additionally, high inoculation rate of heterotrophic algal seed can be utilized as an effective method for contamination control. This two-stage heterotrophic phototrophic process is promising to provide a more efficient way for large scale production of algal biomass and biofuels.     

Two-stage system for hydrogen production by immobilized cyanobacterium Gloeocapsa alpicola CALU 743

Previous studies showed that cell suspensions of unicellular nondiazotrophic cyanobacterium G. alpicola grown under nitrate-limiting conditions intensively produces H2 via fermentation of endogenous glycogen with hydrogen yield more then 90% of theoretical maximum (3.8 mol H2 per mol glucose). H2 production is realized by a Hox hydrogenase on the stages of NAD(P)H generation. Exploiting this property, the two-stage cyclic system for sustained hydrogen production was developed using a photobioreactor (PhBR) with G. alpicola immobilized on glass fiber TR-0.3. Immobilization of the cells on the matrix occurred during growth directly in PhBR operated in continuous mode; the density of culture immobilized achieved 37 g Chl alpha cm(-2). The first stage of the cycle was the photosynthetic incubations of G. alpicola in the flow of the culture medium, which contained limiting concentrations of nitrate for efficient glycogen accumulation and activation of hydrogenase. The second stage was the fermentation of glycogen, with H2 production realized in darkness with continuous Ar sparging and without medium flow. Standardization of optimal parameters for both stages provided a stable cyclic regime of the system: photosynthesis (24 hours)-fermentation (24 hours). The total amount of H2 evolved in one cycle was 957.6 mL L(-1)(matrix), and the overage rate of H2 production during the cycle (48 hours) was about 20 mL h(-1) L(-1)(matrix). Ten consequent cycles was carried out in this regime with reproducible H2 production, although PhBR with the same sample of immobilized culture was operated over a period of more then three months.