Reaction equilibrium of penicillin G with amberlite LA-2 in a nonpolar organic solvent

Studies have been made of the reactive extraction of penicillin G by Amberlite LA-2, a secondary amine, dissolved in kerosene. On the basis of the previous works about extraction equilibria of monocarboxylic acids by some secondary amines in low polar organic solvents, four equilibrium models were suggested to describe the reaction equilibrium of penicillin G in the liquid-liquid extraction system. The calculated results from the models were compared with the experimental data of 96 runs, and only two equilibrium models seemed to be probable. Ultimately, the most reasonable extraction equilibrium model was chosen through spectroscopic studies on organic solutions obtained by five specific extraction equilibrium experiments.     

Recovery of penicillin G from fermentation broth with reactive extraction in a mixer-settler

Summary In a laboratory countercurrent mixer-settler, penicillin was recovered from its fermentation broth by extraction with Amberlite LA-2 in n-butylacetate at pH 5.0 and reextracted from the ion-pair complex containing a solvent phase with a buffer at 7.2–7.5 with an overall degree of extraction above 90 %.Symbols A amine - AHP complex - c concentration - C partition coefficent - E degree of extraction - HP penicillin acid - K_G equilibrium constant - P, P^– penicillin acid anion Indices aq aqueous phase - org organic phase - A amine - AHP complex - G overall - HP free acid - P penicillin     

Equilibrium modeling of extractive enzymatic hydrolysis of penicillin G with concomitant 6-aminopenicillanic acid crystallization

In the present downstream processing of penicillin G, penicillin G is extracted from the fermentation broth with an organic solvent and purified as a potassium salt via a number of back-extraction and crystallization steps. After purification, penicillin G is hydrolyzed to 6-aminopenicillanic acid, a precursor for many semisynthetic beta-lactam antibiotics. We are studying a reduction in the number of pH shifts involved and hence a large reduction in the waste salt production. To this end, the organic penicillin G extract is directly to be added to an aqueous immobilized enzyme suspension reactor and hydrolyzed by extractive catalysis. We found that this conversion can exceed 90% because crystallization of 6-aminopenicillanic acid shifts the equilibrium to the product side. A model was developed for predicting the equilibrium conversion in batch systems containing both a water and a butyl acetate phase, with either potassium or D-p-hydroxyphenylglycine methyl ester as counter-ion of penicillin G. The model incorporates the partitioning equilibrium of the reactants, the enzymatic reaction equilibrium, and the crystallization equilibrium of 6-aminopenicillanic acid. The model predicted the equilibrium conversion of Pen G quite reasonably for different values of pH, initial penicillin G concentration and phase volume ratio. The model can be used as a tool for optimizing the enzymatic hydrolysis.     

Simultaneous extraction and concentration of penicillin G by hollow fiber renewal liquid membrane

In this article, hollow fiber renewal liquid membrane (HFRLM) technique was used for recovery of penicillin G from aqueous solution. The organic solution of 7 vol % di‐n‐octylamine (DOA) + 30 vol % iso‐octanol + kerosene was used as liquid membrane phase, and Na₂CO₃ aqueous solution was used as stripping phase. Experiments were performed as a function of carrier concentration in the organic phase, organic/aqueous volume ratio, pH, and initial penicillin G concentration in the feed phase, pH in the stripping phase, flow rates, etc. The results showed that the HFRLM process was stable and could carry out simultaneous extraction and concentration of penicillin G from aqueous solutions. As a carrier facilitated transport process, the addition of DOA in organic phase could greatly enhance the mass transfer rate; and there was a favorable organic/aqueous volume ratio of 1:20 to 1:30 for this system. The mass transfer flux and overall mass transfer coefficient increased with decreasing pH in the feed phase and increasing pH in the stripping phase, because of variation of the mass transfer driving force caused by pH gradient and distribution equilibrium. The flow rate of the shell side had significant influence on the mass transfer performance, whereas the effect of flow rate of lumen side on the mass transfer performance was slight because of the mass transfer intensification of renewal effect in the lumen side. The results indicated that the HFRLM process was a promising method for the recovery of penicillin G from aqueous solutions. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

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     

Novel reactive perstraction system applied to the hydrolysis of penicillin G

The activity of penicillin acylase has been studied in aqueous and organic solvents, as free enzyme as well as immobilized within the membrane of liquid-core capsules. The activity of the enzyme is inhibited by the accumulation of the products of the hydrolysis reaction, namely phenyl acetic acid (PAA). In order to overcome this inhibition a range of organic solvents were tested for use in in situ product recovery. Of these solvents dibutyl sebacate (DBS) was chosen due to the rapid extraction rate, the high logP and to facilitate capsule production. The extraction efficiency at pH 3.5 for PAA was >80% for phase ratios of >50% free solvent with partition coefficients of 8 and 0.7 for PAA and penicillin G (PenG), respectively, thereby showing that PAA could be selectively extracted at pH 3.5 and 25 degrees C. Liquid-core capsules containing DBS were shown to efficiently remove PAA selectively and the PAA could be effectively back-extracted and the capsules re-used in a three-stage process resulting in high product separation. Immobilization of penicillin acylase onto the capsule membranes resulted in increased operational stability of the enzyme and a very high enzyme activity. Over 53.3% of the PAA formed could be recovered in the capsule core with a concentration over sevenfold higher than in the aqueous phase. Higher extraction efficiencies could be obtained by varying the substrate concentration and number of capsules. The enzyme immobilized on capsules could be stored for over 4 months at pH 8 and 4 degrees C with no loss of activity. Over 80% of the initial activity could be recovered over five repeated batch cycles of the bioconversion process. The importance of capsular perstraction and reactive capsular perstraction has been clearly demonstrated.     

Thermodynamics of the conversion of penicillin G to phenylacetic acid and 6-aminopenicillanic acid

The thermodynamics of the enzymatic conversion (penicillin acylase) of aqueous penicillin G to phenylacetic acid and 6-aminopenicillanic acid have been studied using both high-pressure liquid-chromatography and microcalorimetry. The reaction was carried out in aqueous phosphate buffer over the pH range 6.0-7.6, at ionic strengths from 0.10 to 0.40 mol kg-1, and at temperatures from 292 to 322 K. The data have been analyzed using a chemical equilibrium model with an extended Debye-Hückel expression for the activity coefficients. For the reference reaction, penicillin G- (aq) + H2O(l) = phenylacetic acid-(aq) + 6-aminopenicillanic acid-(aq) + H+ (aq), the following parameters have been obtained: K = (7.35 +/- 1.5) X 10(-8) mol kg-1, delta G0 = 40.7 +/- 0.5 kJ mol-1, delta H0 = 29.7 +/- 0.6 kJ mol-1, and delta C0p = -240 +/- 50 J mol-1 K-1 at 298.15 K and at the thermochemical standard state. The extent of reaction for the overall conversion is highly dependent upon the pH.     

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

Summary 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.     

pH gradients in immobilized amidases and their influence on rates and yields of beta-lactam hydrolysis

The pH gradients developing within immobilized biocatalysts during hydrolysis of penicillin G and glutaryl-7-aminocephalosporanic acid have been estimated both theoretically and experimentally. For the latter a fluorimetric method for the direct measurement of the average pH value within the carrier during reaction has been developed using the pH-dependent fluorescence intensity of an enzyme-bound fluorophore determined with a fiber bundle. The theoretical calculations were based on a model for the hydrolysis with immobilized enzymes using a kinetic expression with five pH-dependent, measurable kinetic and equilibrium constants. The transport reaction differential equation which considers the laminar boundary layer has been solved numerically for the key component. The calculated values agreed well with the experimental data. Under the typical reaction conditions of penicillin G hydrolysis the average pH value in the carrier was 1 and 2.5 pH units below the bulk pH (=8) with and without buffer, respectively. The corresponding changes for the hydrolysis of glutaryl-7-aminocephalosporanic acid at bulk pH 8 in the presence of buffer was 0.5. This demonstrates the existence of considerable pH gradients in carriers during hydrolytic reactions, even in buffered systems with negligible mass transfer resistance. The low pH value causes suboptimal reaction rates, reduced equilibrium conversion, and reduced enzyme stability. These pH gradients can be minimised by using buffers with pK values approximately equal to the bulk pH used for the hydrolysis. The prediction quality of the model has been tested applying it to fixed bed reactor design. The reduction in rate and yield due to concentration and pH gradients can be overcome with simple measures such as high initial pH value and pH adjustments in segmented or recycling fixed bed reactors. Thus, enzymatic conversions with high yield and high operational effectiveness are achieved.     

Equilibrium studies on enantioselective liquid–liquid extraction of homophenylalanine enantiomers with metal-BINAP complexes

Enantioselective liquid–liquid extraction of homophenylalanine (Hph) enantiomers was investigated with metal-BINAP complexes as enantioselective extractants. The metal complexes were synthesized by the complexation of (s)-2,2′-Bis(diphenylphosphino)-1,1′-binaphthalene (BINAP) with different central ions, among which, copper(I) complex allowed the separation of the Hph enantiomers with the highest operational selectivity. Efficiency of the extraction depends, often strongly, on a number of process variables, including types of organic solvents, pH of the aqueous phase, concentration of host and substrate, and temperature. In order to better understand the extraction process, equilibrium of the system were modeled by a homogeneous reaction model and an interfacial reaction model, respectively. Important parameters required by the modeling, such as complexation equilibrium constant and physical distribution coefficients were determined experimentally. When coupled with the parameters, extraction performance can be predicted by the models. Comparison between the experimental values and the model predictions indicates that the homogeneous reaction model can predict more accurately. By modeling and experiment, an optimal extraction condition concerning pH of 8 and host concentration of 2 mmol/L was obtained with high enantioselective (α) of 1.837 and performance factor (pf) of 0.086.     

固定化青霉素酰化酶在光-pH敏感可回用两水相中裂解青霉素G为6-APA

两水相体系在发展中存在的关键问题是相体系回收困难.由于生产成本及降低污染的原因, 用过的相体系需要回收和重复使用.用环境敏感型溶解可逆聚合物形成可回用两水相体系是当前是为可行的回收方法。本文在光敏感可回用高聚物PNBC与pH敏感型可回用高聚物PADB形成的两水相体系中进行固定化青霉素酰化酶的相转移催化青霉素G产生6-APA的反应。在这个两水相体系中,通过优化,在1% NaCl 存在下,６－ＡＰＡ的分配系数可达5.78。催化动力学显示,达平衡的时间近7h,反应最高得率约85.3%（pH 7.8, 20℃）。较相近条件下的单水相反应得率提高近20%。在反应过程中,通过底物及产物的分配系数检测,发现底物分配系数变化不大,而产物6-APA及苯乙酸的分配系数发生很大变化,从而引起产物的得率变化。在两水相中,底物及产物主要分配在上相,固定化酶分配在下相,底物青霉素G进入下相经酶催化产生的6-APA及苯乙酸又转入上相,从而解除了青霉素酰化酶催化反应的底物及产物抑制作用,达到提高产物得率的效果。此外,采用固定化酶较固定化细胞效率高,占用下相体积小,较游离酶稳定性高,且完全单侧分配在下相。因此,在两水相中进行固定化酶的催化反应具有明显的优越性。形成两水相的高聚物PNBC通过488 nm 的激光照射或经滤光的450nm 光源照射得到回收;pH敏感型成相聚合物PADB可通等电点 4.1沉淀可实现循环利用,高聚物的回收率在95%-98%之间,按此回收率计算,聚合物可使用60次以上。     

A predictive thermodynamic model for the bioreduction of acetophenone to phenethyl alcohol using resting cells of Saccharomyces cerevisiae.

Equilibrium conversions were observed in the range of 60.2-76.0% with different initial compositions of reaction media for the bioreduction of acetophenone using resting cells of Saccharomyces cerevisiae in aqueous solutions at 30 degrees C. The reduction of acetophenone in the cells under anaerobic conditions is considered to be coupled with the oxidation of ethanol to acetate in the cytoplasm. A biphasic thermodynamic model is proposed which includes a nonuniform distribution of reagents across the cell membrane, a transmembrane pH gradient, ideal and nonideal solution models, and a basic reaction stoichiometry (ACP + (1/2) EtOH + (1/2)H2O <--> PEA + (1/2)Ac- + (1/2)H+). The intracellular activity coefficients were based on the Lewis-Randall rule for acetophenone, phenethyl alcohol, and H2O and Henry's law for ethanol, acetate anion, and H+. The overall standard Gibbs free energy was estimated to be -0.11 kcal/mol at a pH 7, 25 degrees C, and 1 atm. The intracellular thermodynamic activity coefficients of acetophenone and phenethyl alcohol were predicted to be 471.2 and 866.4, respectively, using the measured initial distribution coefficients and calculated extracellular activity coefficients. The model reflected a zero Gibbs free energy change at calculated conversions within 4% of the measured equilibrium conversions. The analysis verified the effect of the concentration ratio of the substrate acetophenone to the co-substrate ethanol on the conversion efficiency and suggested that the intracellular pH and the pH gradient across the cell transmembrane significantly affect the predicted equilibrium conversion. The intracellular pH of resting, viable cells of Bakers' yeast at the bioconversion conditions was determined experimentally to be 5.77.     

Process optimization of chiral extraction of 2,3-diphenylpropionic acid by experiment and simulation

This paper reports the process optimization of chiral extraction of 2,3-diphenylpropionic acid (2,3-2-PPA) enantiomers by experiment and simulation in centrifugal contactor separators. An efficient extraction system was obtained firstly through single-stage extraction experiments and single-stage extraction model, where sulfobutylether-β-cyclodextrin (SBE-β-CD) and 1,2-dichlorethane were selected as the optimal extractant and organic solvent, respectively. The mechanism of the extraction system was proposed and the thermodynamic constants such as physical partition coefficient and reactive equilibrium constants were obtained. Based on phase and reactive equilibrium as well as the law of mass conservation, a model describing the fractional extraction process was acquired. The process of symmetrical separation of 2,3-2-PPA enantiomers was optimized by the fractional extraction model. The optimal conditions composed of flow rate ratio (W/O) of 3.0, pH of 3.00 and SBE-β-CD concentration of 0.10 mol/L were obtained. Under this case, equal enantiomeric excess (ee_eq) can reach up to 37% at 10 stages. The simulated results reveal that the minimum series for ee_eq > 97% and ee_eq > 99% was 78 and 102, respectively.     

Interactions of two amphiphilic penicillins with myoglobin in aqueous buffered solutions: a thermodynamic and spectroscopy study

The interactions and complexation process of the amphiphilic penicillins sodium cloxacillin and sodium dicloxacillin with horse myoglobin in aqueous buffered solutions of pH 4.5 and 7.4 have been examined by equilibrium dialysis, zeta-potential, isothermal titration calorimetry (ITC) and UV-Vis absorbance techniques. A more opened structure of the protein molecules is detected as a consequence of the reduction of pH from 7.4 to 4.5. Binding isotherms and derived Hill coefficients reflect a cooperative binding behavior. Gibbs energies of binding per mole of drug were obtained from equilibrium dialysis data and compared with those derived from the zeta potential taking into account cooperativity. DeltaGads degrees values so obtained are large and negative at low concentrations where binding to the "high-energy" sites occurs and decreases with the drug concentration. The enthalpies of binding have been obtained from ITC and are small and exothermic so that the Gibbs energies of binding are dominated by large increases in entropy consistent with hydrophobic interactions. Other thermodynamic quantities of the binding mechanism, that is, entropy, DeltaSITCi, Gibbs energy, DeltaGITCi, the binding constant, KITCi, and the number of binding sites, ni, were also obtained, confirming the above results. From ITC data and following a theoretical model, the number of bound and free penicillin molecules was calculated, being higher at pH 4.5 than at pH 7.4. The binding of penicillin causes a conformational transition on protein structure as a consequence of the resulting intramolecular repulsion between the penicillin molecules bound to the protein. Thermodynamic quantites (the Gibbs energy of the transition in water, DeltaGw degrees , and in a hydrophobic environment, DeltaGhc degrees) of the denaturation process were calculated, indicating that at pH 4.5 some of the histidine residues are protonated, becoming accessible to solvent and giving rise to a more opened protein structure.     

Equilibrium position, kinetics, and reactor concepts for the adipyl-7-ADCA-hydrolysis process

One of the building blocks of cephalosporin antibiotics is 7-amino-deacetoxycephalosporanic acid (7-ADCA). It is currently produced from penicillin G using an elaborate chemical ring-expansion step followed by an enzyme-catalyzed hydrolysis. However, 7-ADCA-like components can also be produced by direct fermentation. This is of scientific and economic interest because the elaborate ring-expansion step is performed within the microorganism. In this article, the hydrolysis of the fermentation product adipyl-7-ADCA is studied. Adipyl-7-ADCA can be hydrolyzed in an equilibrium reaction to adipic acid and 7-ADCA using glutaryl-acylase. The equilibrium reaction yield is described as a function of pH, temperature, and initial adipyl-7-ADCA concentration. Reaction rate equations were derived for adipyl-7-ADCA-hydrolysis using three (pH-independent) reaction rate constants and the apparent equilibrium constant. The reaction rate constants were calculated from experimental data. Based on the equilibrium position and reaction rate equations the hydrolysis reaction was optimized and standard reactor configurations were evaluated. It was found that equilibrium yields are high at high pH, high temperature and low-initial adipyl-7-ADCA concentration. The course of the reaction could be described well as a function of pH (7-9), temperature (20-40 degrees C) and concentration using the reaction rate equations. It was shown that a series of CSTR's is the best alternative for the process.     

Study of the factors affecting the extraction of soybean protein by reverse micelles

In this work, the forward and back extraction of soybean protein by reverse micelles was studied. The reverse micellar systems were formed by anionic surfactant sodium bis(2-ethyl hexyl) sulfosuccinate (AOT), isooctane and KCl solution. The effects of AOT concentration, aqueous pH, KCl concentration and phase volume ratio on the extraction efficiency of soybean protein were tested. Suitability of reverse micelles of AOT and Triton-X-100/AOT mixture in organic solvent toluene for soybean protein extraction was also investigated. The experimental results lead to complete forward extraction at the AOT concentration 120 mmol l⁻¹, aqueous pH 5.5 and KCl concentration 0.8 mol l⁻¹. The backward extraction with aqueous phase (pH 5.5) resulted in 100% extraction of soybean protein from the organic phase.     

Extractive separation of penicillin G by facilitated transport via carrier supported liquid membranes

The facilitated transport of penicillin G (Pen G), through a supported liquid membrane with Amberlite LA-2 dissolved in 1-decanol, supported on a microporous polypropylene membrane, were studied. The distribution coefficient was obtained from a batch extraction experiment. The effects of flow rate, carrier concentration, initial concentration of Pen G, and the pH of feed and stripping phases on the transport rate of Pen G through the supported liquid membrane were also investigated. The results are in agreement with theoretical predictions, and it is demonstrated that the transport of Pen G through the supported liquid membrane is controlled simultaneously by mass transfer across both aqueous and liquid membranes. (c) 1993 John Wiley & Sons, Inc.     

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     

A geometric interpretation of the feasibility of reactive extraction/re-extraction of penicillin G.

The reactive extraction (re-extraction) of penicillin G from reaction mixtures is based on complexation with a carrier and subsequent dissociation of the complex. An established mathematical model for this has been analysed to develop a feasibility domain within which the process may be designed and optimised. Geometric and physical interpretations of this domain are provided.     

Multi-stage laccase extraction and separation using aqueous two-phase systems: Experiment and model

This work presents results of experimental and model investigation of continuous multi-stage enzyme extraction using aqueous two-phase systems for the first time. The aqueous two-phase system comprised polyethylene glycol 3000 and phosphate with additional sodium chloride buffered to pH 7. Two different laccases served as model enzymes. One of the laccases was directly taken from fungal culture supernatant, while the other laccase was solubilized lyophilisate. The modeling is based on an equilibrium stage approach. Equilibrium data were taken from single-stage experiments and approximated by different correlation equations. The model describes densities, phase equilibrium, enzyme activity partitioning between the phases. Moreover it allows to consider activity changes due to the aqueous two-phase system. Eight multi-stage mixer-settler experiments under varying operation conditions were performed to validate the proposed model; whereas the total throughput of all multi-stage extraction experiments was about 350 g h⁻¹. The average relative deviation of modeled activities from experimentally measured activities was 23%. Therefore, the model is able to calculate the behavior of the phases as well as the partitioning of the two enzymes between the two phases for a multi-stage process based on single-stage data.