Reactive Extraction Of Penicillin Research Articles

Extraction equilibria of penicillin G in four different types of organic solvent systems

Equilibrium experiments for physical and reactive extraction of penicillin G were carried out with varying pH, overall penicillin concentration and overall amine concentration in liquid–liquid extraction systems with four different types of organic solvents, i.e. amphiprotic solvent, hydrogen-bond donor solvent, hydrogen-bond acceptor solvent, and nonpolar organic solvent. Also, physical and reactive extraction equilibrium models were suggested to find the appropriate equilibrium model for each organic solvent type. By comparison between the experimental data and the calculated results from the extraction equilibrium models, the most probable physical and reactive extraction equilibrium models were determined. The physical extraction equilibrium models for all types of the organic solvents except for nonpolar organic solvent reflected solute–solvent interaction, while the reactive extraction equilibrium models were dependent on the organic solvent type.

Reactive extraction of penicillin G in hollow-fiber and hollow-fiber fabric modules.

Penicillin G (Pen G) can be rapidly extracted in hollow-fiber liquid-liquid contactors using N-lauryl-N-trialkylmethylamine (Amberlite LA-2) as the extractant. n-Butylacetate is much better than decanol as a diluent for such an extraction, although decanol can give a partition coefficient four times larger. The overall mass transfer coefficient found is a function of aqueous flow on the lumen side of the fiber, and is less dependent on shell-side flow. In backextraction, the overall mass transfer coefficient determined is only one tenth that of the forward extraction, primarily because the hydrophobic hollow fibers used have a high mass transfer resistance under these conditions. The mass transfer experiments show that hollow-fiber extraction of Pen G is competitive with centrifugal extraction. The prospects for extraction of other fermentation products with hollow fibers can be estimated based on the present study.

Reactive Extraction of Penicillin G: Selection of Volume Ratios between Phases and Optimum Carrier Concentration

Abstract Reactive extraction of penicillin G at pH 5 and reextraction at pH 7–8 were performed using Amberlite LA-2 (carrier) in n-butyl acetate. The volume ratios of aqueous feed phase to organic extract phase in extraction and organic extract phase to aqueous strip phase in reextraction were varied, and the effects on the degree of extraction and enrichment were studied. The effects of initial concentration ratio of carrier to penicillin G were also investigated. It was found that there existed an optimum carrier concentration giving the maximum degree of extraction and enrichment. Procedure for the selection of volume ratios and concentration ratio at a desired degree of extraction and enrichment was described for initial penicillin G concentration of 10 mmol·dm−3, and generalized to be applicable for any concentrations of penicillin G. Finally, sodium carbonate solution was successfully applied as an aqueous strip phase on behalf of buffer solution in reextraction to avoid the disadvantages of using buffer solution and to shorten the reextraction time.

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.

Reactive extraction of penicillin G in a pilot plant Karr-column III. Modelling and simulation of the extraction process

The longitudinal concentration profiles of penicillin the continuous aqueous phase of a pilot plant Karr-column of 7.6 m height was calculated by a mathematic model consisting of reaction rate and cascase models. Satisfactory agreements between calculated and measured profiles were found. The identified mass transfer coefficients are identical in the bench-scale and pilot plant columns, in the model medium and fermentation medium as well as at different stroke frequencies. The specific interfacial area are strongly influenced by these parameters. The model can be used for calculation of penicillin extraction columns of different sizes. For the layout of the columns, hydrodynamic data are needed, which, however, cannot yet be calculated on a theoretical basis.

Experiments on reactive extraction of penicillin G from fermentation broth : F. Vinczi and J. Bálint, BIOGAL Pharmaceutical Works, Debrecen, Hungary:

Experiments on reactive extraction of penicillin G from fermentation broth : F. Vinczi and J. Bálint, BIOGAL Pharmaceutical Works, Debrecen, Hungary:

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

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.

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

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%.

Reactive extraction of penicillin I: Stability of penicillin G in the presence of carriers and relationships for distribution coefficients and degrees

The decomposition of penicillin G as a function of time, pH, solvent and carrier type is explored and the optimum pH range for penicillin recov Relationships for distribution coefficients and degrees of extraction are devised and evaluated as functions of the concentrations of penicillin and ca