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     

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     

Kinetics of reextraction of Penicillin G from the organic phase after reactive extraction

The kinetics of reextraction of penicillin from the LA-2-penicillin complex-n-butylacetate solution by phosphate buffer was investigated experimentally and theoretically. The concentration time functions can be described by a mathematical model in a wide range of pH-values and complex concentrations.List of Symbols a _P [m²/m³] specific interfacial area - c _A , c _Ai [mMol] concentration of amine in the bulk of the organic phase and at the interface - c _AHP , c _AHPi [mMol] concentration of the complex in bulk of the organic phase and at the interface - c _H , c _Hi [mMol] concentration of the proton in the bulk of the aqueous phase and at the interface - c _P , c _Pi [mMol] concentration of the penicillin acid anion in the bulk of the aqueous phase and at the interface - J _A , J _AHP , J _P [mMol · cm · s^–1] fluxes of amine, complex and penicillin acid anion - k _A , k _AHP , k _P [cm · s^–1] mass transfer coefficients of amine, complex and penicillin acid anion - K _G [mMol²] equilibrium constant - t [k] extraction time     

Analysis of penicillin V biosynthesis during fed-batch cultivations with a high-yielding strain of Penicillium chrysogenum

Metabolites (both intra- and extracellular) involved in penicillin biosynthesis were measured during fed-batch cultivations with a high-yielding strain of Penicillium chrysogenum. The fed-batch cultivations were carried out on a complex medium containing corn steep liqour. Three distinct phases were observed: (a) a rapid growth phase where free amino acids present in the medium are metabolized, (b) a linear growth phase, and (c) a stationary phase. The specific penicillin production (r _p) is initially high and, during the rapid growth phase, it increases slightly. During the linear growth phase r _p is approximately constant [4–6 mg penicillin V (g dry weight)^–1 h^–1 depending on the operating conditions], whereas it decreases during the stationary phase. During the cultivations the tripeptide Aad-Cys-Val (the first metabolite in penicillin biosynthesis) and 8-hydroxypenillic acid (formed by carboxylation of 6-aminopenicillanic acid, 6-APA) were found to accumulate in the medium, whereas the concentrations of isopenicillin N and 6-APA were found to be approximately constant and low. About 3% of the Aad-Cys-Val formed in the first step of the penicillin biosynthetic pathway is lost to the medium and 4% of the isopenicillin N formed in the second step of the pathway is lost as extracellular isopenicillin N, 6-APA or 8-hydroxypenillic acid. Also the cyclic form of -aminoadipic acid, 6-oxopiperidine-2-carboxylic acid, was found to accumulate in the medium and it was found to be formed in an approximately constant ratio to penicillin V of 6 mol/100 mol.     

Microcalorimetric investigations of the metabolism of yeasts. Growth in chemostat cultures on glucose

Summary As part of a project on the production of penicillin, the penicillin production of two strains of Penicillium chrysogenum which have a different penicillin productivity was investigated in bubble column bioreactors and for comparison in stirred fermenters. The main interest of this study were the complicated interrelations between the stirrer speed, the stirrer type, the shear stress, the morphology of the mycelium and broth viscosity as well as the effect of the oxygen transfer behavior on antibiotic productivity.Stirred tank reactors with different turbine stirrers as well as with a draught tube and propeller were employed.The main variable investigated was the stirrer speed. At low stirrer speeds, gas dispersion is inadequate and the insufficient oxygen transfer rate is a limiting factor. At higher stirrer speeds, the oxygen supply of pulpy mycelia is improved and more cell mass is formed. This result is the same for both strains in all three reactors.If the oxygen partial pressure is near the lower cirtical value, a high percentage of the carbon source is converted into penicillin but the penicillin productivity is low due to a low percentage of penicillin producing cells. At oxygen partial pressures just above 8% saturation, the absolute penicillin productivity is maximal. At higher stirrer speeds and dissolved oxygen concentrations the penicillin production phase is shorter, cell growth is higher and a higher percentage of the carbon source is converted into CO₂.In reactors with a draught tube and propeller, a lower productivity is attained than in those with turbine stirrers.The behavior of the two strains is fairly similar. The higher producing strain, however, has a more distinct separation between its periods of growth and production than does the low producing one. At high stirrer speeds the increase in the cell growth rate is less significant and the substrate yield coefficients are higher for the high producing strain than for the low producing one.Symbols C Dissolved oxygen concentration (mg l^–1) - C^* C at saturation (mg l^–1) - k_La Volumetric mass transfer coefficient (h^–1) - OTR Oxygen transfer rate (mg l^–1 h^–1) - OUR Oxygen uptake rate (mg l^–1 h^–1) - rpm Impeller speed (min^–1) - X (Dry) biomass concentration (g kg^–1) - V_g Volumetric gas flow rate (Nl min^–1) - CMC Carboxymethyl cellulose     

Protein mass transfer studies on a spray column using the PEG-Reppal PES 100 aqueous two-phase system

The characterization of Bovine Serum Albumin mass transfer mechanisms in a spray column using an aqueous two-phase system composed of poly(ethylene glycol) and a modified starch-Reppal PES 100-is done. The poly(ethylene glycol) rich phase is used as the dispersed phase and protein transfer takes place from the dispersed phase to the continuous phase. The effect of dispersed phase superficial velocity, system composition, continuous phase height and distribution system design on either overall protein mass transfer coefficient or column hold-up is described. It is shown that continuous phase superficial velocity and phase composition are the main controlling factors for protein transfer. It is also observed that, with the tested system, only at very low dispersed phase superficial velocities is it possible to operate the spray column as an extraction column. In this system the upper operating limit of the dispersed phase velocity is ten times smaller than in other aqueous two-phase systems.List of Symbols ATPS Aqueous Two-Phase System - BSA Bovine Serum Albumin - C _i kg m^–3 inlet dispersed phase protein concentration - C ₀ kg m^–3 outlet dispersed phase protein concentration - C _d kg m^–3 dispersed phase protein concentration - C _c kg m^–3 continuous phase protein concentration - D m column internal diameter - H hold-up - h, h _d m dispersion height - h ₀ m initial dispersion height (initial continuous phase height) - k _da s^–1 overall mass transfer coefficient - m protein partition coefficient - n number of holes of distribution system - PEG Poly(ethylene glycol) - Q m³ s^–1 dispersed phase volumetric flow rate - S m² column internal area - V m³ dispersion volume A. Venâncio was supported by a JNICT (Junta Nacional de Investigaçäo Científica e Tecnológica) grant.     

Sequential liquid-liquid extraction of d-amino acid oxidase from Trigonopsis variabilis

A method for isolation of d-amino acid oxidase (DAAO) from disrupted Trigonopsis variabilis cells has been developed. In an aqueous two-phase system consisting of PEG6000 (220 g l^–1), potassium phosphate (110 g l^–1, K₂HPO₄ + KH₂PO₄ = 10.1:1, mol mol^–1) and dl-methionine (11 g l^–1), the major portion of cellular proteins (87%) was partitioned into the salt phase. By sequential extraction, 48% of DAAO was recovered in PEG phase, giving a yield of 211 U mg protein^–1.     

Semicontinuous penicillin production by two Penicillium chrysogenum strains immobilized in calcium alginate beads

Summary The growth rates of immobilized Penicillium chrysogenum strains are important in their application to semicontinuous penicillin production. Immobilized P. chrysogenum strains produced about 10–15% less biomass but about 1–2 times more penicillin than free suspended mycelia.In a chemically defined medium an industrial P. chrysogenum strain, S₁, produced about 10–12 times more penicillin than strain ATCC 12690. In a complex medium the immobilized P. chrysogenum S₁ produced about 12% penicillin more than in shaken cultures. In bubble column fermentations, penicillin production was 163% higher in the complex medium than in the chemically defined medium.     

Analysis of pipecolic acid in biological fluids using capillary gas chromatography with electron-capture detection and [H11]pipecolic acid as internal standard

A sensitive and accurate stable isotope dilution assay was developed for the measurement of pipecolic acid in body fluids using capillary gas chromatography with electron-capture detection. The method utilizes [²H₁₁]pipecolic acid as the internal standard. Sample preparation consisted of derivatization in aqueous solution (pH 11.5) of the amine moiety with methyl chloroformate to the N-methylcarbamate, followed by acidic ethyl acetate extraction at pH ≤ 2 and further derivatization of the carboxyl moiety with pentafluorobenzyl bromide, the excess of which was removed by solid-phase extraction. Control values have been determined in the plasma of at-term infants, age > 1 week (n = 21, mean = 1.36 μM, range = 0.47–3.27 μM). The utility of the method was demonstrated by quantitating pipecolic acid in biological fluids derived from patients with peroxisomal disorders. The method was validated against an established electron-capture negative ion mass fragmentographic technique.     

Enantioselective high-performance liquid chromatographic determination of nicardipine in human plasma

A sensitive method for the enantioselective high-performance liquid chromatography (HPLC) determination of nicardipine in human plasma is described. (+)-Nicardipine, (−)-nicardipine and (+)-barnidipine as an internal standard are detected by an ultraviolet detector at 254 nm. Racemic nicardipine in human plasma was extracted by a rapid and simple procedure based on C₁₈ bonded-phase extraction. The extraction samples were purified and concentrated on a pre-column using a C₁ stationary phase and the enantiomers of nicardipine are quantitatively separated by HPLC on a Sumichiral OA-4500 column, containing a chemically modified Pirkle-type stationary phase. Determination of (+)- and (−)-nicardipine was possible in a concentration range of 5–100 ng ml⁻¹ and the limit of detection in plasma was 2.5 ng ml⁻¹. The recoveries of (+)- and (−)-nicardipine added to plasma were 91.4–98.4% and 93.3–96.7%, respectively, with coefficients of variation of less than 9.0 and 9.4% respectively. The method was applied to low level monitoring of (+)- and (−)-nicardipine in plasma from healthy volunteers.     

Removal of toluene in waste gases using a biological trickling filter

The removal of toluene from waste gas was studied in a trickling biofilter. A high level of water recirculation (4.7 m h^–1) was maintained in order to keep the liquid phase concentration constant and to achieve a high degree of wetting. For loads in the range from 6 to 150 g m^–3 h^–1 the maximum volumetric removal rate (elimination capacity) was 35±10 g m^–3 h^–1, corresponding to a zero order removal rate of 0.11±0.03 g m^–2 h^–1 per unit of nominal surface area. The surface removal was zero order above the liquid phase concentrations of approximately 1.0 g m^–3, corresponding to inlet gas concentrations above 0.7–0.8 g m^–3. Below this concentration the surface removal was roughly of first order. The magnitude of the first order surface removal rate constant, k_1A , was estimated to be 0.08–0.27 m h^–1 (k_1A a=24–86 h^–1). Near-equilibrium conditions existed in the gas effluent, so mass transfer from gas to liquid was obviously relatively fast compared to the biological degradation. An analytical model based on a constant liquid phase concentration through the trickling filter column predicts the effluent gas concentration and the liquid phase concentration for a first and a zero order surface removal. The experimental results were in reasonable agreement with a very simple model valid for conditions with an overall removal governed by the biological degradation and independent of the gas/liquid mass transfer. The overall liquid mass transfer coefficient, K_La, was found to be a factor 6 higher in the system with biofilm compared to the system without. The difference may be explained by: 1. Difference in the wetting of the packing material, 2. Mass transfer occurring directly from the gas phase to the biofilm, and 3. Enlarged contact area between the gas phase and the biofilm due to a rough biofilm surface.     

Cyanide as a copper and quinone-directed inhibitor of amine oxidases from pea seedlings (<Emphasis Type="Italic">Pisum sativum</Emphasis>) and<Emphasis Type="Italic"> Arthrobacter globiformis</Emphasis>: evidence for both copper coordination and cyanohydrin derivatization of the quinone cofactor

The interactions of cyanide with two copper-containing amine oxidases (CuAOs) from pea seedlings (PSAO) and the soil bacterium Arthrobacter globiformis (AGAO) have been investigated by spectroscopic and kinetic techniques. Previously, we rationalized the effects of azide and cyanide for several CuAOs in terms of copper coordination by these exogenous ligands and their effects on the internal redox equilibrium TPQ_amr-Cu(II)TPQ_sq-Cu(I). The mechanism of cyanide inhibition was proposed to occur through complexation to Cu(I), thereby directly competing with O₂ for reoxidation of TPQ. Although cyanide readily and reversibly reacts with quinones, no direct spectroscopic evidence for cyanohydrin derivatization of TPQ has been previously documented for CuAOs. This work describes the first direct spectroscopic evidence, using both model and enzyme systems, for cyanohydrin derivatization of TPQ. K_d values for Cu(II)-CN^– and Cu(I)-CN^–, as well as the K_i for cyanide inhibition versus substrate amine, are reported for PSAO and AGAO. In spite of cyanohydrin derivatization of the TPQ cofactor in these enzymes, the uncompetitive inhibition of amine oxidation is determined to arise almost exclusively through CN^– complexation of Cu(I).Abbreviations AGAO Arthrobacter globiformis amine oxidase - APAO Arthrobacter P1 amine oxidase - APT attached proton test - BPAO bovine plasma amine oxidase - CuAO quinone-copper containing amine oxidase - LTQ lysyl tyrosylquinone - MAO monoamine oxidase - PKAO porcine kidney amine oxidase - PPAO porcine plasma amine oxidase - PSAO pea seedling amine oxidase - TPQ 2,4,5-trihydroxyphenylalaninequinone - TPQ_amr TPQ aminoresorcinol - TPQ_imq TPQ iminoquinone - TPQ_ox TPQ oxidized - TPQ_sq TPQ semiquinone - WT wild-typeE.M. Shepard and G.A. Juda contributed equally to this workThis revised version was published online in February 2004: Hansenula polymorpha was not italicised at the end of the Introduction, Equation 3 appeared twice, and the resolution of Scheme 3 was insufficient.An erratum to this article can be found at     

Model for the production of L-tryptophan from L-serine and indole by immobilized cells in a three-phase liquid-impelled loop reactor

Production of L-tryptophan from L-serine and indole catalyzed by Escherichia coli, immobilized in k-carrageenan gel beads, is technically feasible in the liquidimpelled loop reactor (LLR), using an organic solvent, e.g. n-dodecane.With L-serine in large excess intrinsic reaction kinetics is approximately first order with respect to indole, with a reaction constant of 8.5×10^–5 m³ kg _dw ^–1 s^–1.The overall process kinetics is jointly controlled by intrinsic kinetics and by intraparticle mass transfer resistance, which can be quantified using an effectiveness factor.Mass transfer of indole from the organic to the aqueous phase and from the aqueous to the gel phase are relatively fast and thus have negligible influence in the overall process kinetics, under the operational conditions tested. However, they may become important if the process is intensified by increasing the cell concentration in the gel and/or the gel hold-up in the reactor.A simple model which includes indole mass balances over the aqueous and organic phases, mass transfer and reaction kinetics, with parameters experimentally determined in independent experiments, was successful in simulating L-tryptophan production in the LLR.List of Symbols a, b, c coefficients of the equilibrium curve for indole between organic and aqueous phases - A, B, C, D, E, F auxiliary variables used in liquid-liquid mass transfer studies - a _x specific interfacial area referred to the volume of the aqueous phase (m^–1) - A _x interfacial area (m²) - a _Y specific interfacial area referred to the volume of the organic phase (m^–1) - A _Y interfacial area (m²) - C _b substrate concentration in the bulk of the aqueous phase (kg m^–3) - C _e substrate concentration in exit stream (kg m^–3) - C _E biocatalyst concentration referred to the aqueous phase (kg m^–3) - C _{E s} biocatalyst concentration referred to the volume of gel (kg m^–3) - C _s substrate concentration at the gel surface (kgm^–3) - d, e, f coefficients of the equilibrium curve for indole between aqueous and organic phases - dp particle diameter (m) - K ₂ kinetic constant (s^–1) - K ₁ kinetic constant K₂/K_M (kg^–1 m³ s^–1) - K _M Michaälis-Menten constant (kgm^–3) - K _X mass transfer coefficient referred to the aqueous phase (ms^–1) - K _Xa_X volumetric mass transfer coefficient based on the volume of the aqueous phase (s^–1) - k _Y mass transfer coefficient referred to the organic phase (ms^–1) - K _Ya_Y volumetric mass transfer coefficient based on the volume of the organic phase (s^–1) - N _X mass flux of indole from organic to aqueous Phase (kg m^–2s^–1) - N _Y mass flux of indole from aqueous to organic phase (kg m^–2s^–1) - Q _e volumetric flow rate in exit stream (m³s^–1) - Q _f volumetric flow rate in feed stream (m³s^–1) - _obs observed reaction rate (kg s^–1 m^–3) - intrinsic reaction rate (kg s^–1 m^–3) - Re Reynolds number - Sc Schmidt number - Sh Sherwood number - t time (s) - u superficial velocity (m s^–1) - V _max maximum reaction rate (kg s^–1m^–3) - V _S volume of the support (m³) - V _X volume of aqueous phase (m³) - V _Y volume of the organic phase (m³) - X indole concentration in the aqueous phase (kgm^–3) - Y indole concentration in the organic phase (kg m^–3 Greek Letters overall effectiveness factor - _e external effectiveness factor - _i internal effectiveness factor - Thiele module A fellowship awarded to one of us (D.M.R.)by INICT is gratefuly acknowledged.     

The Effect of Modification of Nucleotide-37 on the Interaction of Aminoacyl-tRNA with the A Site of the 70S Ribosome

To estimate the effect of modified nucleotide 37, the interaction of two yeast aminoacyl-tRNAs (Phe-tRNA^Phe _+Y and Phe-tRNA^Phe _–Y) with the A site of complex [70S · poly(U) · deacylated tRNA^Phe in the P site] was assayed at 0–20°C. As comparisons with native Phe-tRNA^Phe _+Y showed, removal of the Y base decreased the association constant of Phe-tRNA^Phe _–Y and the complex by an order of magnitude at every temperature tested, and increased the enthalpy of their interaction by 23 kJ/mol. When the Y base was present in the anticodon loop of deacylated tRNA^Phe bound to the P site of the 70S ribosome, twice higher affinity for the A site was observed for Phe-tRNA^Phe _–Y but not for Phe-tRNA^Phe _+Y. Thus, the modified nucleotide 3" of the Phe-tRNA^Phe anticodon stabilized the codon–anticodon interaction both in the A and P sites of the 70S ribosome.     

Binding of Cu (II), Tb (III) and Fe (III) to chicken ovotransferrin

The kinetics of binding of Cu (II), Tb (III) and Fe(III) to ovotransferrin have been investigated using the stopped-flow technique. Rate constants for the second-order reaction, k ₊, were determined by monitoring the absorbance change upon formation of the metal-transferrin complex in time range of milliseconds to seconds. The N and C sites appeared to bind a particular metal ion with the same rate; thus, average formation rate constants k ₊ (average) were 2.4 × 10⁴ M^–1 s^–1 and 8.3 × 10⁴ M^–1 S ^–1 for Cu (II) and Tb (III) respectively. Site preference (N site for Cu (II) and C site for Tb (III)) is then mainly due to the difference in dissociation rate constant for the metals. Fe (III) binding from Fe-nitrilotriacetate complex to apo-ovotransferrin was found to be more rapid, giving an average formation rate constant k ₊ (average) of 5 × 10⁵ M^–1 s^–1, which was followed by a slow increase in absorbance at 465 nm. This slow process has an apparent rate constant in the range 3 s^–1 to 0.5 s^–1, depending upon the degree of Fe (III) saturation. The variation in the rate of the second phase is thought to reflect the difference in the rate of a conformational change for monoferric and diferric ovotransferrins. Monoferric ovotransferrin changes its conformation more rapidly (3.4s^–1) than diferric ovotransferrin (0.52 s^–1). A further absorbance decrease was observed over a period of several minutes; this could be assigned to release of NTA from the complex, as suggested by Honda et al. (1980).Abbreviations Tf ovotransferrin - NTA nitrilotriacetate Jichi Medical School, School of Nursing, Yakushiji 3311-159, Minamikawachi, Tochigi, 329-04 Japan     

Determination of penicillin G in bovine plasma by high-performance liquid chromatography after pre-column derivatization

A simple, selective, and sensitive liquid chromatographic method with ultraviolet detection was developed for the analysis of penicillin G in bovine plasma. The assay utilizes a simple extraction of penicillin G from plasma (with a known amount of penicillin V added as internal standard) with water, dilute sulphuric acid and sodium tungstate solutions, followed by concentration on a conditioned C₁₈ solid-phase extraction column. After elution with 500 μl of elution solution, the penicillins are derivatized with 500 μl of 1,2,4-triazole—mercuric chloride solution at 65°C for 30 min. The penicillin—mercury mercaptide complexes are separated by reversed-phase liquid chromatography on a C₁₈ column. The method, which has a detection limit of 5 ng/ml (ppb) in bovine plasma, was used to quantitatively measure the concentrations of penicillin G in plasma of steers at a series of intervals after the intramuscular administration of a commercial formulation of procaine penicillin G.     

Simultaneous determination of seven penicillins in muscle, liver and kidney tissues from cattle and pigs by a multiresidue high-performance liquid chromatographic method

A high-performance liquid chromatographic (HPLC) method based on solid-phase extraction (SPE) was developed for determination of amoxicillin, penicillin G (benzylpenicillin), ampicillin, oxacillin, cloxacillin, nafcillin and dicloxacillin in muscle, liver and kidney tissues of pigs and cattle. The compounds were extracted in aqueous solution by precipitation of organic materials with a mixture of sulphuric acid and sodium tungstate. The extract was cleaned up by SPE on a divinylbenzene-co-N-vinylpyrrolidone polymeric sorbent. Further clean-up was performed by liquid–liquid partition with diethyl ether. The extract was derivatised with benzoic anhydride and 1,2,4-triazole mercury (II) reagent. Chromatography was performed by reversed-phase gradient HPLC on a C₁₈ column with ultraviolet detection at 323 nm. The limits of detection estimated by a conservative model were in the range 8.9–11.1 μg/kg for amoxicillin, penicillin G, ampicillin, oxacillin, cloxacillin and nafcillin and 18.3–20.9 μg/kg for dicloxacillin. The mean recovery range was 66–77% for amoxicillin, 73–75% for penicillin G, 81–82% for ampicillin, 73–76% for oxacillin, 74–75% for cloxacillin, 66–72% for nafcillin and 58–65% for dicloxacillin.     

The production of lactic acid from whey permeate byLactobacillus helveticus

Summary The effect of pH on growth and lactic acid production ofLactobacillus helveticus was investigated in a continuous culture using supplemented whey ultrafiltrate. Maximum lactate productivity of 5 gl^–1h^–1 occurred at pH 5.5. Whey permeates concentrated up to four times were fermented using batch cultures. Maximum lactic acid concentration of 95 gl^–1 was attained, but residual sugars indicated a possible limitation in growth factors.Nomenclature D Dilution rate [h^–1] - X Biomass [gl^–1] - Glu Glucose consentration [gl^–1] - Gal Galactose consentration [gl^–1] - S Substrate, Lactose consentration [gl^–1] - P Product, Lactate consentration [gl^–1] - Y_p/s Yield, defined as P/S [gg^–1] - r_i Rate of synthesis or consumption of i [gl^–1h^–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     

Fermentative production of P(3HB-co-3HV) from propionic acid by Alcaligenes eutrophus in fed-batch culture with pH-stat continuous substrate feeding method

The feeding of propionic acid for production of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) [P(3HB-co-3HV)] by Alcaligenes eutrophus ATCC17697 was optimized using a fed-batch culture system. The concentration of propionic acid was maintained at 3 g l^–1 as growth was inhibited by propionic acid in the broth. A pH-stat substrate feeding system was used in which propionic acid was fed automatically to maintain a pH of the culture broth at 7.0. By feeding a substrate solution containing 20% (w/v) propionic acid, 4.9% (w/v) ammonia water [at a molar ratio of carbon to nitrogen (C/N molar ratio) of 10] in cell growth phase, the concentration of propionic acid in the broth was maintained at 3 g l^–1 giving a specific growth rate of 0.4 h^–1. To promote P(3HB-co-3HV) production, two stage fed-batch culture which consisted of the stage for the cell growth and the stage for the P(3HB-co-3HV) accumulation was carried out. When the substrate solution whose C/N molar ratio was 50 was fed in P(3HB-co-3HV) accumulation phase, the cell concentration and the P(3HB-co-3HV) content in the cells reached 64 g l^–1 and 58% (w/w) in 55.5 h, respectively.