Immobilization of invertase on a new type of macroporous glycidyl methacrylate

Invertase was immobilized via its carbohydrate moiety. The immobilized enzyme has a specific activity of 5500 IU g^–1, with 45% activity yield on immobilization. In a packed bed reactor, 90% 2.5 M sucrose was converted at a flow rate of 4 bed volumes h^–1. The obtained specific productivity at 40 °C of 3 kg l^–1 h^–1 is the best one so far. Long-term stability was 290 days in 2.5 M sucrose at 40 °C and at a flow rate of 3 bed volumes h^–1.     

Chromatography of human prothrombin from Nitschmann fraction III on Q Sepharose Fast Flow using axial and radial flow column

An axial column (Hitrap Q 5 ml, 2.5 2 1.6 cm) and a radial flow column (3.5 2 5 cm) packed with Q Sepharose Fast Flow media had been evaluated for the separation of human prothrombin. Nitschmann fraction III dissolved in buffered saline (0.10 M sodium chloride buffered with 0.06 M Tris/HCl to pH 7.5) was the starting material. Effects of sample flow rate of the two columns were screened. Under radial flow conditions using the radial column, sample flow rate up to 15 ml/min (i.e. 18 bed volumes/h) was achieved and the operating pressure was below 0.2 MPa eventhough the elution velocity was 30 ml/min. Breakthrough capacity was determined by analyzing the total protein and prothrombin activity of the target protein-containing fraction under subsaturating conditions and both columns had almost the same breakthrough capacity per ml media, indicating that the sample loading was independent of radial column geometry. It was concluded that the radial column is an attractive alternate to traditional axial packed bed column, exhibiting very good potential for use in the separation of human prothrombin.     

Miniaturised expanded-bed column with low dispersion suitable for fast flow-ELISA analyses

Flow-ELISA measurements of the monoclonal antibody concentration in cultivation broth containing murine hybriboma cells were carried out using a small expanded-bed column (0.5×2.5 cm) charged with protein A. A new specialised pellicular agarose/stainless steel matrix designed for high flow rates with fast mass transport properties was used. Special care was taken to get an efficient flow distribution. The axial dispersion coefficient was very low (2×10^–6 m² s^–1 for latex particles at a linear velocity of 10 cm min^–1). Breakthrough curves for polyclonal IgG on the protein A-derivatised support (at 2–11 cm min^–1) further emphasised its advantageous properties. No significant change in dynamic capacity was found over the entire speed range.     

Anion exchange purification of plasmid DNA using expanded bed adsorption

Recent developments in gene therapy with non-viral vectors and DNA vaccination have increased the demand for large amounts of pharmaceutical-grade plasmid DNA. The high viscosity of process streams is of major concern in the purification of plasmids, since it can cause high back pressures in column operations, thus limiting the throughput. In order to avoid these high back pressures, expanded bed anion exchange chromatography was evaluated as an alternative to fixed bed chromatography. A Streamline 25 column filled with 100 ml of Streamline QXL media, was equilibrated with 0.5 M NaCl in TE (10 mM Tris, 1 mM EDTA, pH=8.0) buffer at an upward flow of 300 cmh^-1, E. coli lysates (obtained from up to 3 liters of fermentation broth) were injected in the column. After washing out the unbound material, the media was allowed to sediment and the plasmid was eluted with 1 M NaCl in TE buffer at a downward flow of 120 cmh^-1. Purification factors of 36±1 fold, 26±0.4 plasmid purity, and close to 100% yields were obtained when less than one settled column volume of plasmid feed was injected. However, both recovery yield and purity abruptly decreased when larger amounts were processed–values of 35±2 and 5±0.7 were obtained for the recovery yield and purity, respectively, when 250 ml of feedstock were processed. In these cases, gel clogging and expansion collapse were observed. The processing of larger volumes, thus larger plasmid quantities, was only possible by performing an isopropanol precipitation step prior to the chromatographic step. This step led to an enhancement of the purification step.     

Estimation of cardiac output and stroke volume from thermal equilibration and heartbeat rates in fish

Cardiac output and stroke volume were estimated for a 200 g largemouth blackbass (Micropterus salmoides) by a modified whole-body thermodilution method using the relation between thermal equilibration rates and heartbeat frequencies. The reciprocal of the thermal time constant, k (min^–1), was related to the heartbeat frequency, F (beats min^–1), by the equation k=0.00146 F + 0.309; the slope is the weight-specific stroke volume (ml g^–1) and the intercept is the weight-specific heat transfer constant (cal °C^–1 min^–1 g^–1). Stroke volume was 0.292 ml (0.00146 ml/g body weight), yielding cardiac output values ranging from 44 ml kg^–1 min^–1 (at 30 beats min) to 158 ml kg^–1 min^–1 (at 108 beats min^–1), or 4.4 to 15.8% of body weight. Active (convective) heat transfer due to blood flow constituted an estimated 11 to 34% (mean 22.5%) of total heat transfer, depending on heartbeat frequency; this variability constitutes physiological thermoregulation.     

Chromatography of hen egg-white proteins on anion-exchange cellulose at high flow rates using a radial flow column.

The influence of column configuration on the separation of hen egg-white proteins using Whatman DE52 and QA52 anion-exchange cellulose has been investigated. Using a 100 ml volume axial flow column (6.6 cm x 4.4 cm i.d.) we achieved flow rates of up to 25 ml/min i.e. 15 bed volumes/h after which higher flow was restricted due to pressure constraints within the system. Under radial flow conditions using a 100 ml column flow rates of up to 150 ml/min i.e. 90 bed volumes/h were achieved using DE52 and QA52. While chromatographic resolution was superior under axial flow at the lower flow rates excellent resolution was maintained at up to 150 ml/min using the radial flow column. This is a consequence of the fast kinetics of adsorption/desorption exhibited by DE52 and QA52. The data indicate that it is the column configuration and not the cellulose matrix which influences flow performance.     

Ethanol tolerance in free and sol-gel immobilised Saccharomyces cerevisiae

The tolerance of sol-gel immobilised and free Saccharomyces cerevisiae to ethanol was studied. The effects of ethanol preincubation time showed that the specific death velocity decreased from 2×10⁵ c.f.u. min^–1 for free cells to 2×10⁴ c.f.u. min^–1 for immobilised cells thus indicating that immobilised yeast was far less sensitive to the ethanol damage. The specific glucose consumption of immobilised and free cells on a per cell basis was 3×10^–12 g cell^–1 h^–1 and 9×10^–12 g cell^–1 h^–1, respectively.     

Antibiotic production by the immobilized cyanobacterium,Scytonema sp. TISTR 8208, in a seaweed-type photobioreactor

A photobioreactor was constructed using either anchored polyurethane foam strips (1 × 1 × 40 cm, PU-strips) fixed on a stainless-steel ring to prevent flotation, or free-floating polyurethane foam blocks (1 × 1 × 1 cm, PU-blocks) as biomass supporting materials (BSM). The cyanobacterium,Scytonema sp. TISTR 8208, which produces an antibiotic, was immobilized onto PU-strips or -blocks. The free-floating PU-blocks could immobilize only about 70% of the total cells, while the anchored PU-strips could immobilize as much as 97%. PU-strips were chosen as the BSM and we named this type of reactor, seaweed-type bioreactor (STB). Optimal physical conditions for antibiotic production were determined in the STB. Inoculum density was 0.4 g l^–1 and cells were sparged with air containing 5% CO₂ circulated at the gas flow rate of 250 ml min^–1 and illuminated at a light intensity of 200 mol photon m^–2 s^–1. The production of antibiotic could be increased 3-fold.Author for correspondence     

Expanded bed adsorption for recovery of patatin from crude potato juice

An expanded bed adsorption process was used to isolate patatin possessing esterase activity, from a crude juice of potato tubers. Patatin is the major storage protein of potato tubers and is released in ample amounts in the processing effluent during starch milling. We employed mixed mode affinity resins, where the binding depends primarily on the pH, and is almost independent of the ionic strength. From a library of mixed mode chemistries involving both charged and hydrophobic functions, we screened for ligands with binding specificity for patatin. The dynamic binding capacity of two high density (1.45–1.5 g ml^-1) patatin-binding agarose-glass resins in response to change of linear velocity (85–230 cm h^-1) was tested in packed (25 ml) and expanded (250 ml) column modes. The column operation included a loading step at low expansion; H/H_o~1.2. Adsorption from crude juice at pH 7.5, retained patatins up to a breakthrough level of 50%. The eluate fraction at pH 3.5, now effectively stripped from the pigments, provided a 2.5-fold enzyme enrichment and produced 4 g protein per cycle. Column productivity was 122 kAU L^-1 h^-1. The study, using potato juice as model feedstock, demonstrated the feasibility of expanded bed-recovery of potentially valuable proteins from plant biomass.This revised version was published online in October 2005 with corrections to the Cover Date.     

Large-scale separation of magnetic bioaffinity adsorbents

Flat magnetic separator was used to separate magnetic bioaffinity adsorbents from litre volumes of suspensions. Both magnetic cross-linked erythrocytes and magnetic chitosan were efficiently separated; at least 95% adsorbent recovery was achieved at maximum flow rate (1680 ml min^–1). Using this system low amounts of trypsin were concentrated from large sample volumes using magnetic erythrocytes as affinity adsorbent.     

Control of renal and extrarenal salt and water excretion by plasma angiotensin II in the kelp gull (Larus dominicanus)

Summary The osmoregulatory effects of intravenously (i.v.) administered angiotensin II (AII) at dose rates of 5, 15 and 45 ng · kg^–1 · min^–1 were examined in kelp gulls utilizing salt glands and/or kidneys as excretory organs.In birds given i.v. infusion of 1200 mOsmolal NaCl at 0.3 ml · min^–1 and utilizing only the salt glands to excrete the load, infusion of AII for 30 min consistently inhibited salt gland function in a dose-dependent manner.In birds given i.v. infusion of 500 mOsmolal NaCl at 0.72 ml · min^–1 and utilizing both salt glands and kidneys to excrete the load, each dose of AII given for 2 h inhibited salt gland function but stimulated the kidney, so that the overall outputs of salt and water were enhanced and showed significant (2P<0.01) positive correlations with plasma AII.In birds given i.v. infusion of 200 mOsmolal glucose at 0.5 ml · min^–1 and utilizing only the kidneys to excrete the load, low doses of AII (5 and 15 ng · kg^–1 · min^–1) caused renal salt and water retention, whereas a high dose (45 ng · kg^–1 · min^–1) stimulated salt and water output.The actions of plasma AII in kelp gulls support the concept that this hormone plays a vital role in avian osmoregulation, having effects on both salt gland and kidney function. Elevation of plasma AII consistently inhibits actively secreting salt glands, but its effects upon renal excretion depend primarily on the osmotic status as well as on the plasma AII concentration. In conditions of salt and volume loading doses of AII stimulate sodium and water excretion. With salt and volume depletion, the action of AII is bi-phasic with low doses promoting renal sodium and water retention but high circulating levels causing natriuresis and diuresis.     

Continuous culture of the hyperthermophilic archaeum Pyrococcus furiosus

Summary A system for continuous culture of the hyperthermophilic archaeum Pyrococcus furiosus in the absence of elemental sulphur has been developed. An all-glass gas-lift bioreactor was used to provide high mass transfer at low shear forces, whilst eliminating the potential for corrosion. Steady-state cell densities of P. furiosus were found to increase with higher inert gas flow rates, reaching a maximum in this system with 0.5 vol. vol^–1 min^–1 of nitrogen (N₂). N₂ permitted higher cell densities than the other inert gases tested (argon, helium and sulphur hexafluoride) under equivalent conditions. At 0.5 vol. vol^–1 min^–1 of N₂ a cell density in excess of 3 × 10⁹ ml^–1 could be maintained indefinitely at a dilution rate of 0.2 h^–1. Higher dilution rates gave progressively lower steady-state cell densities. Teh biomass production was maximal, however, at a dilution rate of 0.4 h^–1. At this dilution rate the bioreactor was able to generate more than 1.5 g wet weight of cells h^–1 l^–1 culture volume.Correspondence to: N. Raven     

Conversion of cellulose into fungal cell mass

Summary Chaetomium cellulolyticum (ATCC 32319) was cultivated on glucose, Avicel and/or Sigmacell in a 20-1 stirred tank batch reactor. The substrate (cellulose) concentration, the cell mass concentration (through protein and/or nitrogen content), reducing sugar concentration, the enzyme activity, the alkali consumption rate, the dissolved O₂ and CO₂ concentrations in the outlet gas were measured. The specific growth rate, the substrate yield coefficient, cell productivity, the oxygen consumption rate, the CO₂ production rate and the volumetric mass transfer coefficient were determined. At the beginning of the growth phase the oxygen utilization rate exhibits a sharp maximum. This maximum could be used to start process control. Because of the long lag phase periodic batch operation is recommended.Symbols CP cell protein concentration (g l^–1) - FPA FP enzyme activity (IU l^–1) - GP dissolved protein concentration (g l^–1) - IU international unit of enzyme activity - k_La volumetric mass tranfer coefficient (h^–1) - LG alkali (1 n NaOH) consumption (ml) - LGX specific alkali consumption rate per cell mass (ml g^–1 h^–1) - P cell mass productivity (g l^–1 h^–1) - specific oxygen consumption rate per cell mass (g g^–1 h^–1) - Q aeration rate (volumetric gas flow rate per volume of medium, vvm) (min^–1) - N impeller speed (revolution per minute, rpm) (min^–1) - S substrate concentration (g l^–1) - S⁰ S at t_F=0 (g l^–1) - S₀ S in feed (g l^–1) - SR acid consumption (ml) - TDW total dry weight (g l^–1) - T temperature (° C) - t_F cultivation time (h) - U substrate conversion - X cell mass concentration (g l^–1) - Y_X/S vield coefficient - specific growth rate (h^–1) - _m maximum specific growth rate (h^–1)     

Use of swimming speed and egg ratio as predictors of the status of rotifer cultures in aquaculture

This study evaluated the use of egg ratio (eggs rotifer^–1) and swimming speed (mm min^–1) as prediction criteria for production and culture quality in mass cultures of the rotifer Brachionus plicatilis. Egg ratio was determined to be a suitable predictor of rotifer growth and production in the cultures. Low egg ratios (i.e., 0–0.17 eggs rotifer^–1) indicate reduced rotifer population over time (i.e., negative net population growth rates). However, at this time egg ratio dynamics are not suitably understood to predict in advance a sudden population collapse.Swimming speed of reproductive, egg-carrying females in the exponential growth phase was 40–45 mm min^–1. During exponential growth swimming speed was independent of the food used. Lower swimming speeds were obtained in late stationary phase (10–25 mm min^–1) when yeast was used as a food source. Both environmental factors (e.g., accumulating metabolites) and changes in nutritional state of the rotifers may have affected the swimming speed, but environmental factors appear to be the most important. We believe that swimming speed has the potential of becoming an accurate predictor of culture quality in mass cultures of rotifers.     

Development of a gradient elution high-performance liquid chromatography assay with ultraviolet detection for the determination in plasma of the anticancer peptide [Arg, -Trp, mePhe]-substance P (6–11) (antagonist G), its major metabolites and a C-terminal pyrene-labelled conjugate

[Arg⁶, -Trp^7,9, mePhe⁸]-substance P (6–11), code-named antagonist G, is a novel peptide currently undergoing early clinical trials as an anticancer drug. A sensitive, high efficiency high-performance liquid chromatography (HPLC) method is described for the determination in human plasma of antagonist G and its three major metabolites, deamidated-G (M1), G-minus Met¹¹ (M2) and G[Met¹¹(O)] (M3). Gradient elution was employed using 40 mM ammonium acetate in 0.15% trifluoroacetic acid as buffer A and acetonitrile as solvent B, with a linear gradient increasing from 30 to 100% B over 15 min, together with a microbore analytical column (μBondapak C₁₈, 30 cm×2 mm I.D.). Detection was by UV at 280 nm and the column was maintained at 40°C. Retention times varied by <1% throughout the day and were as follows: G, 13.0 min; M1, 12.2 min; M2, 11.2 min; M3, 10.8 min, and 18.1 min for a pyrene conjugate of G (G–P). The limit of detection on column (LOD) was 2.5 ng for antagonist G, M1–3 and G–P and the limit of quantitation (LOQ) was 20 ng/ml for G and 100 ng/ml for M1–3. Sample clean-up by solid-phase extraction using C₂-bonded 40 μm silica particles (Bond Elut, 1 ml reservoirs) resulted in elimination of interference from plasma constituents. Within-day and between-day precision and accuracy over a broad range of concentrations (100 ng/ml–100 μg/ml) normally varied by <10%, although at the highest concentrations of M1 and M2 studied (50 μg/ml), increased variability and reduced recovery were observed. The new assay will aid in the clinical development of antagonist G.     

Effects of stream order and season on mineralization of [14C]-phenol in streams

Mineralization of trace levels of [¹⁴C]-phenol by heterotrophic microorganisms was quantified at 4 sites along a river continuum in southwestern Virginia. Significant phenol mineralization rates were detected in surface sediment and seston samples at all sites from August 1985 through May 1986. Phenol degradation was strongly affected by season (ANOVA; P < 0.0001). From a baseline rate in August (range: 1.19 × 10^-5 to 897 × 10^-4 mg phenol mineralized mg AFDW^-1 h^-1) phenol mineralization rose to a yearly maximum in October (range: 1.21 × 10^-4 to 1.16 × 10^-3 mg phenol mineralized mg AFDW^-1 h^-1) despite decreasing stream temperatures. This autumnal peak in phenol degradation was attributed to the pulsed input of allochthonous detritus, especially leaf litter, which contains substantial quantities of phenols and related compounds. Although phenol mineralization was significant in these streams, phenols were metabolized at much slower rates than more labile compounds present in the dissolved organic matter (DOM) pool. Estimates of turnover rates for three major components of DOM revealed that glucose and glutamate turnover rates (0.064–0.140 h^-1 mg sediment AFDW^-1 and 0.140–0.610 h^-1 mg sediment AFDW^-1, respectively) were, respectively, 2.2–4.7 × and 9.6–16.9 × greater than phenol turnover rates (0.015–0.064 h^-1 mg sediment AFDW^-1). Although the relatively low rates of utilization of refractory phenolic materials suggest that these compounds may accumulate and become more prevalent components of the DOM pool, phenol concentrations at the 4 study sites remained below detectable levels (i.e., < 1 g 1^-1) throughout the study. Consequently, it seems that although phenolic materials are metabolized more slowly than labile DOM, phenols are degraded at rates which preclude accumulation in the water column.     

Simulation of a multicolumn recirculated packed bed reactor (MRPBR) for penicillin acylase

Enzyme reactors for the industrial hydrolysis of penicillin are analyzed in terms of biocatalyst stability to pH. A multicolumn system with packed beds placed in parallel and operating under recirculating conditions is proposed as an adequate reactor for this process. The system is studied both experimentally and with the aid of a simulation program.List of Symbols A transversal area (cm²) - C _A ammonia concentration in the reaction mixture (M) - C ₁ concentration of KH₂PO₄ in buffer (M) - C ₂ concentration of K₂HPO₄ in buffer (M) - d _p biocatalyst diameter (cm) - E enzyme or biocatalyst concentration (gcat l^–1) - K _APA APA non competitive inhibition constant (M) - K _IS excess substrate inhibition constant (M) - Km constant Michaelis-Menten (M) - K _PAA PAA competitive inhibition constant (M) - Q recirculation flow rate (cm³ min^–1) - Q _T recirculation flow rate per column (cm³ min^–1) - Re Reynolds number - S _E substrate concentration entering the neutralization tank (M) - S ₀ initial substrate concentration (M) - S _T substrate concentration in neutralization tank (M) - t time (min) - v _i initial reactor rate (mol min^–1 gcat^–1) - V _s superficial velocity (cm seg^–1) - V _T volume of neutralization tank (cm³) - X _E substrate conversion entering tank - X _T substrate conversion in neutralization tank - X conversion - Z reactor length (cm) - z axial position in reactor (cm) - z ^* non-dimensional axial position in reactor - biocatalyst's density (gcat cm^–3) - p pressure drop in the packed-bed reactor     

Response surface optimization for the continuous glucose isomerization process

Production of fructose via a continuous glucose isomerization process was optimized using response surface methodology. Glucose isomerization was performed using immobilized glucose isomerase in a flow-through tubular reactor. Process factors eg pH (7.0–7.8), temperature (50–60°C), flow rate (5–17 ml min^–1) and glucose content (30–50% w/w) of the feedstock solution were simultaneously tested according to a central composite experimental design. Measured responses such as % isomerization, and fructose yield (gh^–1) has an excellent correlation with tested factors. The highest desirability,D, (geometric mean of % isomerization and fructose yield) was obtained when the feedstock (56–60°C) had 34–36% glucose, a pH of 7.4–7.8 and was pumped at 15 ml min^–1.     

Preparation and characterisation of Cibacron Blue F3G-A poly(ethylene) hollow-fibre affinity membranes

Poly(ethylene) hollow-fibre membranes with immobilised Cibacron Blue F3G-A were obtained in four different ways from epoxy-activated fibres. Membranes with a maximum capacity of 26 mg lysozyme ml^–1and a dye density of 52 mol ml^–1were obtained when ammonia was used to open the epoxy group before dye immobilisation. Pure water flux of the modified membranes at 1 bar pressure was 1.0 cm min^–1, thus meaning only a reduction of 1.5-fold with regard to the unmodified membranes. The support-dye bond was stable as judged by the unmodified capacity of the membranes and the negligible amount of dye leaked after 520 h of exposure to 6 M urea in 0.5 M NaOH.