Design of metabolic engineering strategies for maximizing L-(-)-carnitine production by Escherichia coli. Integration of the metabolic and bioreactor levels

In this work metabolic engineering strategies for maximizing L-(-)-carnitine production by Escherichia coli based on the Biochemical System Theory and the Indirect Optimization Method are presented. The model integrates the metabolic and the bioreactor levels using power-law formalism. Based on the S-system model, the Indirect Optimization Method was applied, leading to profiles of parameter values that are compatible with both the physiology of the cells and the bioreactor system operating conditions. This guarantees their viability and fitness and yields higher rates of L-(-)-carnitine production. Experimental results using a high cell density reactor were compared with optimized predictions from the Indirect Optimization Method. When two parameters (the dilution rate and the initial crotonobetaine concentration) were directly changed in the real experimental system to the prescribed optimum values, the system showed better performance in L-(-)-carnitine production (74% increase in production rate), in close agreement with the model's predictions. The model shows control points at macroscopic (reactor operation) and microscopic (molecular) levels where conversion and productivity can be increased. In accordance with the optimized solution, the next logical step to improve the L-(-)-carnitine production rate will involve metabolic engineering of the E. coli strain by overexpressing the carnitine transferase, CaiB, activity and the protein carrier, CaiT, responsible for substrate and product transport in and out of the cell. By this means it is predicted production may be enhanced by up to three times the original value.     

Epigenetic regulation of carnitine metabolising enzymes in Proteus sp. under aerobic conditions

Proteus sp. is able to catalyse the reversible transformation of crotonobetaine into L(-)-carnitine during aerobic growth. Contrary to other Enterobacteriaceae no reduction of crotonobetaine into gamma-butyrobetaine could be detected in the culture supernatants. Activities of L(-)-carnitine dehydratase, carnitine racemasing system and crotonobetaine reductase could be determined enzymatically in cell-free extracts of Proteus sp. Small amounts of gamma-butyrobetaine were found in cell-free extracts, indicating that it accumulates in the cell and inhibits the crotonobetaine reductase. Crotonobetaine and L(-)-carnitine were able to induce enzymes of carnitine metabolism. gamma-Butyrobetaine and glucose repress carnitine metabolism in Proteus sp. Other betaines are neither inducers nor repressors. Monoclonal antibodies against purified CaiA from Escherichia coli O44K74 recognise an analogous protein in cell-free extract of Proteus sp. No cross-reactivity could be detected with monoclonal antibodies against purified CaiB and CaiD from E. coli O44K74.     

Cloning, nucleotide sequence, and expression of the Escherichia coli gene encoding carnitine dehydratase.

Carnitine dehydratase from Escherichia coli O44 K74 is an inducible enzyme detectable in cells grown anaerobically in the presence of L-(-)-carnitine or crotonobetaine. The purified enzyme catalyzes the dehydration of L-(-)-carnitine to crotonobetaine (H. Jung, K. Jung, and H.-P. Kleber, Biochim. Biophys. Acta 1003:270-276, 1989). The caiB gene, encoding carnitine dehydratase, was isolated by oligonucleotide screening from a genomic library of E. coli O44 K74. The caiB gene is 1,215 bp long, and it encodes a protein of 405 amino acids with a predicted M(r) of 45,074. The identity of the gene product was first assessed by its comigration in sodium dodecyl sulfate-polyacrylamide gels with the purified enzyme after overexpression in the pT7 system and by its enzymatic activity. Moreover, the N-terminal amino acid sequence of the purified protein was found to be identical to that predicted from the gene sequence. Northern (RNA) analysis showed that caiB is likely to be cotranscribed with at least one other gene. This other gene could be the gene encoding a 47-kDa protein, which was overexpressed upstream of caiB.     

Metabolism of L(−)-carnitine by Enterobacteriaceae under aerobic conditions

Different Enterobacteriaceae, such as Escherichia coli, Proteus vulgaris and Proteus mirabilis, are able to convert L(-)-carnitine, via crotonobetaine, into gamma-butyrobetaine in the presence of carbon and nitrogen sources under aerobic conditions. Intermediates of L(-)-carnitine metabolism (crotonobetaine, gamma-butyrobetaine) could be detected by thin-layer chromatography. In parallel, L(-)-carnitine dehydratase, carnitine racemasing system and crotonobetaine reductase activities were determined enzymatically. Monoclonal antibodies against purified CaiB and CaiA from E. coli O44K74 were used to screen cell-free extracts of different Enterobacteriaceae (E. coli ATCC 25922, P. vulgaris, P. mirabilis, Citrobacter freundii, Enterobacter cloacae and Klebsiella pneumoniae) grown under aerobic conditions in the presence of L(-)-carnitine.     

Synthesis of l(-)-carnitine by hydration of crotonobetaine by enterobacteria

Summary Enterobacteria, especially Escherichia coli, Salmonella typhimurium and Proteus vulgaris, are capable of forming l(-)-carnitine by hydration of the double bond of crotonobetaine under anaerobic conditions. The carnitine hydrolyase is an inducible cytosolic enzyme which catalyses either the dehydration of l-carnitine or the hydration of crotonobetaine. In growing cultures, the addition of fumarate to a complex or minimal medium stimulated l-carnitine synthesis by diminishing the reduction of crotonobetaine to -butyrobetaine. However, l-carnitine synthesis was repressed after addition of nitrate or under aerobic conditions. If the carnitine hydrolyase was induced by l-carnitine or crotonobetaine, these respiratory chain electron acceptors did not impair carnitine formation by resting cells, indicating an epigenetical regulation of carnitine synthesis. Using this bacterial pathway for the biosynthesis of l-carnitine, conditions for producing a high yield are described. The method has some advantages in comparison with other biochemical or microbiological procedures for the production of l-carnitine.Dedicated to Professor Dr. H.-J. Rehm on the occasion of his 60th birthday     

Stimulation of the anaerobic growth ofSalmonella typhimurium by reduction ofl-carnitine,carnitine derivatives and structure-related trimethylammonium compounds

In view of the development of al-carnitine deficiency, the metabolism ofl-carnitine and structure-related trimethylammonium compounds was studied inSalmonella typhimurium LT₂ by means of thin-layer chromatography (TLC).l-Carnitine, crotonobetaine and acetyl-l-carnitine stimulated the anaerobic growth in a complex medium significantly. The stimulation depended on the formation of -butyrobetaine. The reduction ofl-carnitine proceeded in two steps: (1) Dehydration of thel-carnitine to crotonobetaine, (2) hydrogenation of crotonobetaine to -butyrobetaine. The reduction of crotonobetaine was responsible for the growth stimulation. Terminal electron acceptors of the anaerobic respiration such as nitrate and trimethylamine N-oxide, but not fumarate, suppressed the catabolism ofl-carnitine completely. Glucose fermentation, too, inhibited the reduction ofl-carnitine but optimal growth with a high carnitine catabolism was achieved byd-ribose. The esters of carnitine with medium- and long-chain fatty acids inhibited the growth considerably because of their detergent properties.Abbreviations TLC thin-layer chromatography     

Crotonobetaine reductase from Escherichia coli consists of two proteins

Crotonobetaine reductase from Escherichia coli is composed of two proteins (component I (CI) and component II (CII)). CI has been purified to electrophoretic homogeneity from a cell-free extract of E. coli O44 K74. The purified protein shows l(-)-carnitine dehydratase activity and its N-terminal amino acid sequence is identical to the caiB gene product from E. coli O44 K74. The relative molecular mass of CI has been determined to be 86100. It is composed of two identical subunits with a molecular mass of 42600. The isoelectric point of CI was found to be 4.3. CII was purified from an overexpression strain in one step by ion exchange chromatography on Fractogel EMD TMAE 650(S). The N-terminal amino acid sequence of CII shows absolute identity with the N-terminal sequence of the caiA gene product, i.e. of the postulated crotonobetaine reductase. The relative molecular mass of the protein is 164400 and it is composed of four identical subunits of molecular mass 41500. The isoelectric point of CII is 5.6. CII contains non-covalently bound FAD in a molar ratio of 1:1. In the crotonobetaine reductase reaction one dimer of CI associates with one tetramer of CII. A still unknown low-molecular-mass effector described for the l(-)-carnitine dehydratase is also necessary for crotonobetaine reductase activity. Monoclonal antibodies were raised against the two components of crotonobetaine reductase.     

Link between primary and secondary metabolism in the biotransformation of trimethylammonium compounds by escherichia coli

The aim of this work was to understand the steps controlling the process of biotransformation of trimethylamonium compounds into L(-)-carnitine by Escherichia coli and the link between the central carbon or primary and the secondary metabolism expressed. Thus, the enzyme activities involved in the biotransformation process of crotonobetaine into L(-)-carnitine (crotonobetaine hydration reaction and crotonobetaine reduction reaction), in the synthesis of acetyl-CoA (pyruvate dehydrogenase, acetyl-CoA synthetase, and ATP:acetate phosphotransferase) and in the distribution of metabolites for the tricarboxylic acid (isocitrate dehydrogenase) and glyoxylate (isocitrate lyase) cycles, were followed in batch with both growing and resting cells and during continuous cell growth in stirred-tank and high-cell-density membrane reactors. In addition, the levels of carnitine, crotonobetaine, gamma-butyrobetaine, ATP, NADH/NAD(+), and acetyl-CoA/CoA ratios were measured to determine how metabolic fluxes were distributed in the catabolic system. The results provide the first experimental evidence demonstrating the important role of the glyoxylate shunt during biotransformation of resting cells and the need for high levels of ATP to maintain metabolite transport and biotransformation (2.1 to 16.0 mmol L cellular/mmol ATP L reactor h). Moreover, the results obtained for the pool of acetyl-CoA/CoA indicate that it also correlated with the biotransformation process. The main metabolic pathway operating during cell growth in the high cell-density membrane reactor was that related to isocitrate dehydrogenase (during start-up) and isocitrate lyase (during steady-state operation), together with phosphotransacetylase and acetyl-CoA synthetase. More importantly, the link between central carbon and L(-)-carnitine metabolism at the level of the ATP pool was also confirmed.     

Biotransformation of crotonobetaine to L(–)-carnitine in Proteus sp.

Two proteins, component I (CI) and component II (CII), catalyze the biotransformation of crotonobetaine to L(-)-carnitine in Proteus sp. CI was purified to electrophoretic homogeneity from cell-free extracts of Proteus sp. The N-terminal amino acid sequence of CI showed high similarity (80%) to the caiB gene product from Escherichia coli O44K74, which encodes the L(-)-carnitine dehydratase. CI alone was unable to convert crotonobetaine into L(-)-carnitine even in the presence of the cosubstrates crotonobetainyl-CoA or gamma-butyrobetainyl-CoA, which are essential for this biotransformation. The relative molecular mass of CI was determined to be 91.1 kDa. CI is composed of two identical subunits of molecular mass 43.6 kDa. The isoelectric point is 5.0. CII was purified to electrophoretic homogeneity from cell-free extracts of Proteus sp. and its N-terminal amino acid sequence showed high similarity (75%) to the caiD gene product of E. coli O44K74. The relative molecular mass of CII was shown to be 88.0 kDa, and CII is composed of three identical subunits of molecular mass 30.1 kDa. The isoelectric point of CII is 4.9. For the biotransformation of crotonobetaine to L(-)-carnitine, the presence of CI, CII, and a cosubstrate (crotonobetainyl-CoA or gamma-butyrobetainyl-CoA) were shown to be essential.     

Development and evaluation of efficient recombinant Escherichia coli strains for the production of 3‐hydroxypropionic acid from glycerol

3‐Hydroxypropionic acid (3‐HP) is a commercially valuable chemical with the potential to be a key building block for deriving many industrially important chemicals. However, its biological production has not been well documented. Our previous study demonstrated the feasibility of producing 3‐HP from glycerol using the recombinant Escherichia coli SH254 expressing glycerol dehydratase (DhaB) and aldehyde dehydrogenase (AldH), and reported that an “imbalance between the two enzymes” and the “instability of the first enzyme DhaB” were the major factors limiting 3‐HP production. In this study, the efficiency of the recombinant strain(s) was improved by expressing DhaB and AldH in two compatible isopropyl‐thio‐β‐galactoside (IPTG) inducible plasmids along with glycerol dehydratase reactivase (GDR). The expression levels of the two proteins were measured. It was found that the changes in protein expression were associated with their enzymatic activity and balance. While cloning an alternate aldehyde dehydrogenase (ALDH), α‐ketoglutaric semialdehyde dehydrogenase (KGSADH), instead of AldH, the recombinant E. coli SH‐BGK1 showed the highest level of 3‐HP production (2.8 g/L) under shake‐flask conditions. When an aerobic fed‐batch process was carried out under bioreactor conditions at pH 7.0, the recombinant SH‐BGK1 produced 38.7 g 3‐HP/L with an average yield of 35%. This article reports the highest level of 3‐HP production from glycerol thus far. Biotechnol. Bioeng. 2009; 104: 729–739 © 2009 Wiley Periodicals, Inc.     

High-density Escherichia coli cultures for continuous l(−)-carnitine production

The use of a biological procedure for l-carnitine production as an alternative to chemical methods must be accompanied by an efficient and highly productive reaction system. Continuous l-carnitine production from crotonobetaine was studied in a cell-recycle reactor with Escherichia coli O44 K74 as biocatalyst. This bioreactor, running under the optimum medium composition (25 mM fumarate, 5 g/l peptone), was able to reach a high cell density (26 g dry weight/l) and therefore to obtain high productivity values (6.2 g l-carnitine l⁻¹ h⁻¹). This process showed its feasibility for industrial l-carnitine production. In addition, resting cells maintained in continuous operation, with crotonobetaine as the only medium component, kept their biocatalytic capacity for 4 days, but the biotransformation capacity decreased progressively when this particular method of cultivation was used. Received: 10 December 1998 / Received revision: 19 February 1999 / Accepted: 20 February 1999     

L(-)-carnitine production using a recombinant Escherichia coli strain

The L(-)-carnitine production by biotransformation using the recombinant strain Escherichia coli pT7-5KE32 has been studied and optimized with crotonobetaine and D(+)-carnitine as substrates. A resting rather than a growing cells system for L(-)-carnitine production was chosen, crotonobetaine being the best substrate. High biocatalytic activity was obtained after growing the cells under anaerobic conditions at 37°C and with crotonobetaine or L(-)-carnitine as inducer. The growth incubation temperature (37°C) was high enough as to activate the heat-inducible λp_L promoter inserted in the plasmid pGP1-2. The best biotransformation conditions were with resting cells, under aerobiosis, with 4 g l⁻¹ and 100 mM biomass and substrate concentrations respectively. Under these conditions the biotransformation time (1 h) was shorter and the L(-)-carnitine yield (70%) higher than previously reported. Consequently productivity value (11.3 g l⁻¹h⁻¹) was highly improved when comparing with other published works. The resting cells could be reused until eight times maintaining product yield levels well over 50% that meant to increase ten times the L(-)-carnitine obtained per gram of biomass.     

Role of energetic coenzyme pools in the production of L-carnitine by Escherichia coli

The aim of this work was to understand the steps controlling the biotransformation of trimethylammonium compounds into L(-)-carnitine by Escherichia coli. The high-cell density reactor steady-state levels of carbon source (glycerol), biotransformation substrate (crotonobetaine), acetate (anaerobiosis product) and fumarate (as an electron acceptor) were pulsed by increasing them fivefold. Following the pulse, the evolution of the enzyme activities involved in the biotransformation process of crotonobetaine into L(-)-carnitine (crotonobetaine hydration), in the synthesis of acetyl-CoA (ACS: acetyl-CoA synthetase and PTA: ATP: acetate phosphotransferase) and in the distribution of metabolites for the tricarboxylic acid (ICDH: isocitrate dehydrogenase) and glyoxylate (ICL: isocitrate lyase) cycles was monitored. In addition, the levels of carnitine, the cell ATP content and the NADH/NAD(+) ratio were measured in order to assess the importance and participation of these energetic coenzymes in the catabolic system. The results provided an experimental demonstration of the important role of the glyoxylate shunt during biotransformation and the need for high levels of ATP to maintain metabolite transport and biotransformation. Moreover, the results obtained for the NADH/NAD(+) pool indicated that it is correlated with the biotransformation process at the NAD(+) regeneration and ATP production level in anaerobiosis. More importantly, a linear correlation between the NADH/NAD(+) ratio and the levels of the ICDH and ICL (carbon and electron flows) and the PTA and ACS (acetate and ATP production and acetyl-CoA synthesis) activity levels was assessed. The main metabolic pathway operating during cell metabolic perturbation with a pulse of glycerol and acetate in the high-cell density membrane reactor was that related to ICDH and ICL, both regulating the carbon metabolism, together with PTA and ACS enzymes (regulating ATP production).     

An indirect optimization method for biochemical systems: description of method and application to the maximization of the rate of ethanol, glycerol, and carbohydrate production in Saccharomyces cerevisiae

Three metabolic models for the production of ethanol, glycerol, and carbohydrates in yeast are optimized with respect to different production rates. While originally nonlinear, all three optimization problems are reduced in such a way that methods of linear programming can be used. The optimizations lead to profiles of enzyme activities that are compatible with the physiology of the cells, which guarantees their viability and fitness, and yield higher rates of the desired final end products than the original systems. In order to increase ethanol rate production at least three times, six enzymes must be modulated. By contrast, when the production of glycerol or carbohydrates is optimized, modulation of just one enzyme (in the case of glycerol) or two enzymes (in the case of carbohydrates) is necessary to yield significant increases in product flux rate. Comparisons of our results with those obtained from other methods show great similarities and demonstrate that both are valid methods. The choice of one or the other method depends on the question of interest. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 758-772, 1997.     

Role of betaine:CoA ligase (CaiC) in the activation of betaines and the transfer of coenzyme A in Escherichia coli

Aims:  Characterization of the role of CaiC in the biotransformation of trimethylammonium compounds into l (−)-carnitine in Escherichia coli .
Methods and Results:  The caiC gene was cloned and overexpressed in E. coli and its effect on the production of l (−)-carnitine was analysed. Betaine:CoA ligase and CoA transferase activities were analysed in cell free extracts and products were studied by electrospray mass spectrometry (ESI-MS). Substrate specificity of the caiC gene product was high, reflecting the high specialization of the carnitine pathway. Although CoA-transferase activity was also detected in vitro , the main in vivo role of CaiC was found to be the synthesis of betainyl-CoAs. Overexpression of CaiC allowed the biotransformation of crotonobetaine to l (−)-carnitine to be enhanced nearly 20-fold, the yield reaching up to 30% (with growing cells). Higher yields were obtained using resting cells (up to 60%), even when d (+)-carnitine was used as substrate.
Conclusions:  The expression of CaiC is a control step in the biotransformation of trimethylammonium compounds in E. coli .
Significance and Impact of the Study:  A bacterial betaine:CoA ligase has been characterized for the first time, underlining its important role for the production of l -carnitine with Escherichia coli .     

Purification and properties of carnitine dehydratase from Escherichia coli--a new enzyme of carnitine metabolization

Carnitine dehydratase from Escherichia coli 044 K74 is an inducible enzyme detectable in cells grown anaerobically in the presence of L(-)-carnitine or crotonobetaine. It has been purified 500-fold to electrophoretic homogeneity by chromatography on phenyl-Sepharose, hydroxyapatite, DEAE-Sepharose, second phenyl-Sepharose and finally gel filtration on a Sephadex G-100 column. During the purification procedure a low-molecular-weight effector essential for enzyme activity was separated from the enzyme. The addition of this still unknown effector caused reactivation of the apoenzyme. The relative molecular mass of the apoenzyme has been estimated to be 85,000. It seems to be composed of two identical subunits with a relative molecular mass of 45,000. The purified and reactivated enzyme has been further characterized with respect to pH and temperature optimum (7.8 and 37-42 degrees C), equilibrium constant (Keq = 1.5 +/- 0.2) and substrate specifity. The enzyme is inhibited by thiol reagents. The Km value for crotonobetaine is 1.2.10(-2) M. gamma-Butyrobetaine, D(+)-carnitine and choline are competitive inhibitors of crotonobetaine hydration.     

High density cultivation of Anchusa officinalis in a stirred-tank bioreactor with in situ filtration

Previously, Su et al. [Biotechnol Bioeng 42: 884–890 (1993)] reported improved production of rosmarinic acid by Anchusa officinalis in shake-flask cultures using a cultivation strategy that involved intermittent medium exchange. Implementation of this cultivation strategy in 2.5-1 stirred-tank bioreactor cultures is investigated in the present study. Intermittent cell/medium separation in the bioreactor was accomplished by means of automated in situ culture filtration. In the bioreactor culture, rosmarinic acid production was found very sensitive to agitation and aeration conditions as well as dissolved oxygen concentration. A maximum cell density of 35 g dry weight/l and a rosmarinic acid concentration of 3.7 g/l were obtained by maintaining the dissolved oxygen concentration above 30% air saturation, gradually raising the impeller tip speed from 34 cm/s to 72 cm/s, and keeping the aeration rate at 0.44 vvm while increasing the O₂: air ratio in the gas feed stream to 4:1. This result is comparable with the data obtained from shake-flask cultures using the same culture strategy.     

Semicontinuous bioreactor production of a recombinant human therapeutic protein using a chemically inducible viral amplicon expression system in transgenic plant cell suspension cultures

Plant cell culture is an alternative for the production of recombinant human therapeutic proteins because of improved product safety, lower production cost, and capability for eukaryotic post‐translational modification. In this study, bioreactor production of recombinant human alpha‐1‐antitrypsin (rAAT) glycoprotein using a chemically inducible Cucumber mosaic virus (CMV) viral amplicon expression system in transgenic Nicotiana benthamiana cell culture is presented. Optimization of a chemically inducible plant cell culture requires evaluation of effects of timing of induction (TOI) and concentration of inducer (COI) on protein productivity and protein quality (biological functionality). To determine the optimal TOI, the oxygen uptake rate (OUR) of the plant cell culture was chosen as a physiological indicator for inducing maximum rAAT expression. Effects of COI on rAAT production were investigated using a semicontinuous culture, which enables the distinction between effects of growth rate and effects of inducer concentration. An optimized semicontinuous bioreactor operation was further proposed to maximize the recombinant protein production. The results demonstrated that the transgenic plant cells, transformed with the inducible viral amplicon expression system, maintain higher OUR and exhibit lower extracellular protease activity and lower total phenolics concentration in the optimized semicontinuous bioreactor process than in a traditional batch bioreactor operation, resulting in a 25‐fold increase in extracellular functional rAAT (603 µg/L) and a higher ratio of functional rAAT to total rAAT (85–90%). Surprisingly, sustained rAAT production and steady state, long‐term bioreactor operation is possible following chemical induction and establishment of the viral amplicons. Biotechnol. Bioeng. 2010; 106: 408–421. © 2010 Wiley Periodicals, Inc.     

Production of a high viscosity polysaccharide, methylan, in a novel bioreactor

The effect of shear stress on the production of a high viscosity polysaccharide, methylan, from methanol by Methylobacterium organophilum was investigated by using a multidisk mixer. It was observed in the multidisk mixer with defined shear stresses that the specific production rate of methylan increased gradually with increasing shear stress up to 30 Pa, and the production rate was constant beyond 30 Pa. This result suggested that the limited mass transfer from the medium into cells reduced methylan production. A novel bioreactor that provided the large volume of a high shear region was used to increase methylan production. Fed-batch cultures in the novel bioreactor were performed by the dissolved oxygen-stat method of methanol. When 1.13 g/L ammonium ion was added, the concentrations of cells of methylan were 31 and 20.6 g/L, respectively. The productions of cells and methylan in our designed bioreactor were 20 and 50% higher than those obtained in a conventional fermentor. The methylan content reached a maximum of 20.7 g/L in the bioreactor and the viscosity of the fermentation broth was 127 Pa . s, which corresponds to 68 g/L as a xanthan. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 54: 115-121, 1997.     

Continuous production of manganese peroxidase by Phanerochaete chrysosporium immobilized on polyurethane foam in a pulsed packed-bed bioreactor

The bottleneck of the application of manganese peroxidase (MnP) on an industrial scale in pulp biobleaching or in degradation of hazardous compounds is the lack of an efficient production system. Three main problems arise for the continuous production of MnP during secondary metabolism of Phanerochaete chrysosporium: enzyme production occurs only under specific physiological conditions corresponding to C or N limitation, high O(2) tension, and adequate Mn(+2) concentration; the enzyme that is produced is destabilized by extracellular proteases; and excessive growth of the mycelium blocks effective oxygen transfer. To overcome these drawbacks, continuous production of MnP was optimized by selecting a suitable bioreactor configuration and the environmental and operating conditions affecting both enzyme production and stability. The combination between a proper feed rate and the application of a pulsation in a packed-bed bioreactor permitted the maintenance of continuous secretion of MnP while limiting mycelial growth and avoiding bed clogging. Environmental factors as an Mn(+2) concentration of 5000 muM and high oxygen tension enhanced MnP production. The hydraulics of the bioreactor corresponding to a plug flow model with partial mixing and an operating hydraulic rentention time of 24 h were optimal to achieve stable operating conditions. This policy allowed long operation periods, obtaining higher productivities than the best reported in the literature. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 56: 130-137, 1997.