Reactive extraction of penicillin G in a pilot plant Karr-column

Summary Penicillin G was extracted from a model medium with a secondary amine (Amberlite LA-2) as carrier in n-butylacetate as solvent in a 7.6 m high pilot plant Karr-column at different stroke frequencies, throughput of the phases, concentrations of Penicillin G and carrier and ratios of the throughputs of the aqueous and organic phases. Up to penicillin concentrations of 30 gl^–1, throughputs of the aqueous phase of 100 lh^–1 and throughput ratios of the aqueous phase-to-organic phase of 3, very high degrees of extraction (99%) can be achieved with a penicillin loss below 1%.Symbols a specific interfacial area with regard to the volume of the continuous phase - C partition coefficient - cA, cA, i concentration of carrier (sec. amine) in the bulk at the interface - cAHP, cAHP, i concentration of complex in the bulk at the interface - cH proton concentration - cHP_a, cHP_a,i concentration of free acid in the bulk of the aqueous phase at the interface - cHP_o, cHP_{o, i} concentration of free acid in the bulk of the organic phase, at the interface - cP, cP, i concentration of acid anions in the bulk of the aqueous phase, at the interface - d₃₂ Sauter droplet diameter - E degree of extraction - f stroke frequency - KG reaction equilibrium constant - K_phys distribution coefficient - N number of stages in cascade - t mean residence time of the aqueous phase - _aq throughput of the aqueous phase - _o throughput of the organic phase - Z dimensionless longitudinal coordinate of the column with regard to its active length (4 m) - holdup of the organic phase     

Continuous acetone-butanol production with direct product removal

Summary To eliminate the product inhibition and increase the productivity of butanol formation, a continuously operated membrane bioreactor was connected to a four-stage mixer-settler cascade. Clostridium acetobutylicum was cultivated in this reactor. Butanol was selectively extracted with butyric acid saturated n-decanol from the cell-free cultivation medium, and the butanol-free medium was refed into the reactor. Due to the high boiling point of decanol, the recovery of butanol from the decanol solution is easy. The partition coefficient and selectivity of butanol in the cultivation medium-decanol-system is sufficiently high for removing it from the medium. Direct contact of the cells with the decanol phase causes cell damage. However, decanol is practically insoluble in the fermentation medium, thus the contact of the cell-free medium with the solvent phase does not influence of cell growth and product formation. At a dilution rate of D _z=0.1 h^-1, the butanol productivity was increased by removing butanol from the medium by a factor of four. A further increase was prevented by a contaminant of the technical decanol, which was identified by GC-MS-analysis as 1-,3-hexandiol.Symbols D dilution rate, h^-1 - D _eff effective dilution rate (Eq. 3), h^-1 - D _Ex extraction dilution rate (Eq. 3), h^-1 - D _g dilution rate of cell suspension in reactor-filter-system, h^-1 - E degree of extraction (Eq. 3), l - P product concentration in medium after extraction, g l^-1 - P _O product concentration in reactor, g l^-1 - R _P productivity and product formation rate, g l^-1 h^-1 - q _p S specific product formation coefficient with regard to the cell growth rate, l - V _F volume of cell suspension in filter module, l - V _g volume of the cell suspension in reactor and in filter module V _g =V _R +V _F , l - V _R volume of cell suspension in ractor, l - v _O cell free feed rate, l h^-1 - v ₁ flow rate of cell suspension leaves the reactor, l h^-1 - v _E flow rate of decanol through the extractor, l h^-1 - v _w flow rate of the cell free medium through the filter modul, l h^-1 - X cell mass concentration, g l^-1 - specific growth rate of the cells, h^-1 Dedicated to Professor Dr. H. J. Rehm on the occasion of his 60th birthday     

Reactive extraction of penicillin G in a pilot plant Karr-column II. Fermentation broths

Summary Penicillin G was extracted from mycelfree fermentation broths by means of the carrier (Amberlite LA-2) in n-butylacetate at pH 5 in a 7.6 m high pilot plant Karr-column with degrees of extraction E=98–99% and penicillin enrichments up to 3. The reextraction was carried out with phosphate buffer at pH-values above 7.5 with degree of extractions E=86–88% and penicillin enrichments up to 3. The penicillin and carrier losses were negligible. The influence of the process variables on the extraction degree was investigated. The penicillin extraction of the model medium and the fermentation broths were compared. Recommendations are given for the optimal penicillin recovery with reactive extraction.Symbols a specific interfacial area with regard to the volume of the continuous phase - cA concentration of carrier - cAHP,O concentration of complex in feed - cP,cP,O concentration of penicillin acid anion in theaqueous phase, in the feed - d ₃₂ Sauter droplet diameter - E degree of extraction - f stroke frequency - V _aq throughput of the aqueous phase - V ₀ throughput of the organic phase - Z dimensionsless longitudinal coordinate of the column with regard to its active length (4m) - holdup of the organic phase     

Glucose as a substrate in recombinant strain fermentation technology

Summary Glucose supplements to complex growth media of Escherichia coli affect the production of a recombinant model protein under the control of a temperature-sensitive expression system. The bacterial Crabtree effect, which occurs in the presence of glucose under aerobic conditions, not only represses the formation of citric acid cycle enzymes, but also represses the formation of the plasmid-encoded product even though the synthesis of this protein is under the control of the temperature-inducible lambda P _R-promoter/cl857-repressor expression system. When the recombinant E. coli is grown at a moderate temperature (35° C) with protein hydrolysate and glucose as substrates, a biphasic growth and production pattern is observed. In the first phase, the cells grow with a high specific growth rate, utilizing glucose and forming glutamate as a byproduct. The intracellular level of recombinant protein is very low in this phase. Later, glutamate is consumed, indicating an active citric acid cycle. The degradation of glutamate is accompanied by the intracellular accumulation of high amounts of recombinant protein.     

Reactive extraction of penicillin G from mycel-containing broth in a countercurrent extraction decanter

Penicillin was recovered from mycel-containing fermentation broth by direct reactive extraction into a counter-current extraction decanter, Type CA 226-290 of the Westfalia Separator Co., at room temperature via steady state operation. Penicillin concentrations in the feed varied from 3 to 41 g L(-1), Amberlite LA-2 carrier concentrations from 7 to 20 g L(-1)and/or DITDA carrier concentrations from 7.2 to 84 g L(-1), the LA-2-to-penicillin mole concentration ratio from 4 to 6.4, and/or the DITDA-to-penicillin mole concentration ratio was maintained at 2. The throughputs of the fermentation broth (520 to 880 L h(-1)) of the solvent phase (200 to 860 L h(-1)) and the over all throughput (800 to 1750 L h(-1)) were high. Extraction degrees of 72 to 96% were achieved between pH 4.6 and 5.1. Without carriers in the same pH range, extraction degrees of only 17 to 19% were attained. By reducing the pH to 2.3 and in the absence of carriers, the degree of extraction was increased to 61%. However, during the extraction, 6.5% of the penicillin decomposed. At these high throughputs, the steady state was attained within 1 to 4 min. Through the mechanical stress, the length of the hyphae was reduced and the protein content of the broth was increased by 50 to 100%. However, this protein content had no appreciable influence on the phase separation.     

Tetracycline production byStreptomyces aureofaciens: the time lag of production

Summary The exact time course of phosphate consumption in a tetracycline production byStreptomyces aureofaciens has been determined. The data have been compared with model simulations according to a model proposed by Votruba et al. (1984). This led to a revision of his equation for the rate of phosphate consumption and to the proposal that phosphate is consumed proportionally to the growth rate. In contradiction to the model simulations it was found that the length of the time lag of the production is independent of the initial phosphate concentration. While the model explains the time lag through inhibition of the production by phosphate, the measured data show that there must be another or an additional reason for the lag. Simultaneously with the start of the production the organism changes from an organic substrate to ammonia as nitrogen source.All experiments have been carried out in a bubble column of 651 working volume as fed batch fermentation. An autoanalyzer and a HPLC was coupled to the reactor for automatic measurement of phosphate, ammonia, sucrose and products in short intervals. Composition of the outlet gas, pH, pO₂, temperature and weight of the substrate flasks were monitored on-line.     

Shift in product formation from acetate to ethanol using metabolic inhibitors inFusarium oxysporum

Summary Fusarium oxysporum 841 produces a mixture of ethanol and acetic acid from glucose, xylose or Avicel (microcrystalline cellulose) substrates. Some metabolic inhibitors viz. sodium azide, dinitrophenol and polyethylene glycol were used for shifting product formation from acetic acid to ethanol. Using these inhibitors 1.5- to 2- fold increase in ethanol production was achieved with significant repression (by 80 to 90%) of acetic acid. Almost theoretical yields of ethanol were obtained.     

Monitoring and control of biotechnological production processes by Bio-FET-FIA-sensors

Summary Single and multisensor field effect transistors (FET) with a pH-sensitive Si/SiO₂/Si₃N₄/Ta₂O₅-gate and reference electrode (for single sensor) were developed and used for manufacturing the following biological (Bio)-FETs: for glucose analysis, glucose oxidase-FET (GOD-FET); for urea analysis, urease-FET; and for cephalosporin C analysis, cephalosporinase-FET. The GOD-FETs were integrated into flow injection analysis (FIA) of the Eppendorf variables analyser (EVA) system and used for monitoring the glucose concentration in microbial cultivation and production processes with recombinant Escherichia coli K12 MF, recombinant E. coli JM103, Saccharomyces cerevisiae H620, and Candida boidinii. Urease-FET-FIA was used to monitor the urea concentration in a simulated cultivation of Cephalosporium acremonium and urease-FET-FIA and GOD-FET-FIA for the monitoring of urea and glucose concentrations in simulated S. cerevisiae cultivations.     

Formation of acetic acid from cellulosic substrates byFusarium oxysporum

Summary Four strains of Fusarium oxysporum and a strain of Monilia brunnae were screened for their ability to convert cellulosic substrates into ethanol/acetic acid. These strains were found to utilize cellulose and produce extracellular cellulases. However, only F. oxysporum 841 was found to convert glucose, xylose, and cellulose into ethanol and acetic acid as major end-products under microaerobic conditions. Acetic acid at a level of 4.7 g/l resulted in a single-step process on potato pulp medium, indicating the potential of the strain for converting cellulosic substrates into acetic acid. Offprint requests to: K. Schügerl