Bioconversion of gitoxigenin by immobilized plant cells in a column bioreactor

Summary Daucus carota cells immobilized in a Ca-alginate performed the bioconversion of gitoxigenin to 5-hydroxygitoxigenin in a column bioreactor. The smooth spherical shape of the alginate beads was preserved for more than three weeks. The bioreactor was functional for more than thirty days as detected by the bioconversion activity. The rate of bioconversion was influenced by means of aeration.Issued as National Research Council of Canada Publication Number 19556     

Ethanol production by nitrogen-deficient yeast cells immobilized in a hollow-fiber membrane bioreactor

Summary Cells ofSaccharomyces cerevisiae ATCC 4126, immobilized within the macroporous walls of asymmetric hollow-fiber membranes, were alternately perfused with 10% glucose complex medium and with 10% glucose defined medium which was deficient in nitrogen. Using complex growth medium, ethanol productivities during the initial 10 h of culture attained a maximum level of 133 g/l-h based on the total fiber volume (3% ethanol). Productivities during nitrogen deficiency stabilized at 10 g/l-h (0.5 ethanol). In subsequent growth phases, ethanol production rates increased to levels 40–70% of initial growth-phase values, but the ability to regenerate the fermentation activity decreased with culture age. During nitrogen deficiency, the fermentation efficiency declined with a concomitant reduction in the total protein concentration of immobilized cells within the hollow-fiber membranes. The molar ratio of acetaldehyde to ethanol increased seven-fold during nitrogen deficiency, indicating that the overall decline in glycolytic activity was accompanied by preferential reduction in alcohol dehydrogenase activity. The molar ratio of glycerol to ethanol increased two-fold during nitrogen deficiency, and large lipid-like droplets accumulated within the nitrogen-deficient cells. In addition to these findings, we conclude that current hollow-fiber membrane reactors should be limited to cell cultures having low growth rates, low O₂ requirements, and low CO₂ production rates.     

Production of precursors for anti-Alzheimer drugs: Asymmetric bioreduction in a packed-bed bioreactor using immobilized D. carota cells

(S)-1-Phenylethanol derivatives, which are the precursors of many pharmacological products, have also been used as anti-Alzheimer drugs. Bioreduction experiments were performed in a batch and packed-bed bioreactor. Then, the kinetics constants were determined by examining the reaction kinetics in the batch system with free and immobilized carrot cells. Also, the effective diffusion coefficient (D_e) of acetophenone in calcium alginate-immobilized carrot cells was investigated. Kinetics constants for free cells, which are intrinsic values, are reaction rate V_max?=?0.052?mmol?L^?1?min^?1, and constants of the Michaelis–Menten K_M?=?2.31?mmol?L^?1. Kinetics constants for immobilized cells, which are considered apparent values, are V_{max, app}?=?0.0407?mmol?L^?1 min^?1, K_{M, app}?=?3.0472?mmol?L^?1 for 2?mm bead diameter, and V_{max, app}?=?0.0453?mmol?L^?1 min^?1, K_{M, app}?=?4.9383?mmol?L^?1 for 3?mm bead diameter. Average value of effective diffusion coefficient of acetophenone in immobilized beads was determined as 1.97?×?10^?6?cm²?s^?1. Using immobilized carrot cells in an up-flow packed-bed reactor, continuous production of (S)-1-phenylethanol through asymmetric bioreduction of acetophenone was performed. The effects of the residence time and concentrations of substrate were investigated at pH 7.6 and 33°C. Enantiomerically pure (S)-1-phenylethanol (ee?>?99%) was produced with 75% conversion at 4-hr residence time.     

Hydrogen production by immobilized cells in the nozzle loop bioreactor

Summary The continuous production of hydrogen in a Nozzle Loop Bioreactor was investigated using immobilized Rhodospirillum rubum KS-301 with glucose as the growth-limiting substrate. The maximum hydrogen production rate in the experimental range was 91mL/h at dilution rate 0.4h^-1, initial glucose concentration 5.4g/L, and circulation rate 70h^-1 .     

A horizontal bioreactor for ethanol production by immobilized cells

Continuous ethanol production in a three stage horizontal tank bioreactor (HTR) by yeast cells entrapped in Ca-alginate was about 30% higher than in a vertical type of bioreactor and reached 31 kg/(m³ · h) at 95% glucose utilization. Maximum ethanol productivity obtained was 41.2 kg/(m³ · h), however, with 38% of the glucose fed to the HTR being wasted. The higher performance of the HTR had been mainly accounted for the reduction of the adverse CO₂ gas phase effect and the more pronounced plug-flow character. Glucose and ethanol profiles along the HTR revealed that 50–80% of the overall fermentation activity was present in the first stage. Within a test period of 23 d the HTR showed an excellent operational stability.Compared to other continuous ethanol production processes using entrapped yeast cells the HTR presented here belongs to the top ones.     

A horizontal bioreactor for ethanol production by immobilized cells

A mathematical model which describes ethanol formation in a horizontal tank reactor containing Saccharomyces cerevisiae immobilized in small beads of calcium alginate has been developed. The design equations combine flow dynamics of the reactor as well as product formation kinetics. The model was verified for 11 continuous experiments, where dilution rate, feed glucose concentration and bead volume fraction were varied. The model predicts effluent ethanol concentration and CO₂ production rate within the experimental error. A simplification of the model is possible, when the feed glucose concentration does not exceed 150 kg/m³. The simplification results in an analytical solution of the design equation and hence can easily be applied for design purposes as well as for optimization studies.     

A horizontal bioreactor for ethanol production by immobilized cells

The one-parameter-tanks-in-series model was found to be an adequate model for the characterization of flow dynamics in a horizontal immobilized cell reactor, when blue dextran was used as tracer. Isobutanol proved to be inadequate, because it diffused inside the beads and thus caused tailing in RTD. The CO₂ evolution rate displayed the most pronounced effect on axial liquid dispersion. At high CO₂ production rates and low dilution rates each stage of the reactor behaved like a well-mixed reactor. At lower CO₂ evolution rates the number of tanks (N) related to the reactor increased up to 10. The medium flow rate affects axial dispersion to a minor degree. An increase of the dilution rate from 0.328 to 1.34 h^?1 resulted in a slight rise of N from 3.5 to 5 at high CO₂ production and from 4 to 7 at medium CO₂ production rates. Variation in the bead hold up showed the same characteristic axial mixing behavior as reflected by changing the medium flow rate. The quantitative correlation between axial mixing and the most significant fermentation parameters (dilution rate, CO₂ evolution rate and bead hold up) allow to develop an overall model, which besides kinetic expressions also contains terms related to the flow dynamics of the reactor. In the third part of this communication such a model will be presented and compared with actual fermentation data.     

Production of monoclonal antibodies by hybridoma cells in a flat sheet membrane bioreactor.

The purpose of this study was to investigate hybridoma growth and monoclonal antibody formation in a flat sheet membrane bioreactor. The effects of several different molecular weight cutoff membranes on growth and antibody formation were investigated. Nutrient and toxic product diffusion through the membranes were quantified, and the kinetic and physical constants of the system were determined.     

Production of carboxylic acids from hydrolyzed corn meal by immobilized cell fermentation in a fibrous-bed bioreactor

Corn meal hydrolyzed with amylases was used as the carbon source for producing acetic, propionic, and butyric acids via anaerobic fermentations. In this study, corn meal, containing 75% (w/w) starch, 20% (w/w) fibers, and 1.5% (w/w) protein, was first hydrolyzed using amylases at 60 degrees C. The hydrolysis yielded approximately 100% recovery of starch converted to glucose and 17.9% recovery of protein. The resulting corn meal hydrolyzate was then used, after sterilization, for fermentation studies. A co-culture of Lactococcus lactis and Clostridium formicoaceticum was used to produce acetic acid from glucose. Propionibacterium acidipropionici was used for propionic acid fermentation, and Clostridium tyrobutylicum was used for butyric acid production. These cells were immobilized on a spirally wound fibrous matrix packed in a fibrous-bed bioreactor (FBB) developed for multi-phase biological reactions or fermentation. The bioreactor was connected to a stirred-tank fermentor that provided pH and temperature controls via medium circulation. The fermentation system was operated at the recycle batch mode. Temperature and pH were controlled at 37 degrees C and 7.6, respectively, for acetic acid fermentation, 32 degrees C and 6.0, respectively, for propionic acid fermentation, and 37 degrees C and 6.0, respectively, for butyric acid production. The fermentation demonstrated a yield of approximately 100% and a volumetric productivity of approximately 1 g/(1 h) for acetic acid production. The propionic acid fermentation achieved an approximately 60% yield and a productivity of 2.12 g/(1 h), whereas the butyric acid fermentation obtained an approximately 50% yield and a productivity of 6.78 g/(1 h). These results were comparable to, or better than those fermentations using chemically defined media containing glucose as the substrate, suggesting that these carboxylic acids can be efficiently produced from direct fermentation of corn meal hydrolyzate. The corn fiber present as suspended solids in the corn meal hydrolyzate did not cause operating problem to the immobilized cell bioreactor as is usually encountered by conventional immobilized cell bioreactor systems. It is concluded that the FBB technology is suitable for producing value-added biochemicals directly from agricultural residues or commodities such as corn meal.     

Gallotannin hydrolysis by immobilized fungal mycelia in a packed bed bioreactor.

Hydrolysis of gallotannin to gallic acid by immobilized mycelia of Aspergillus niger MTCC 282, Aspergillus fischerii MTCC 150, Fusarium solani MTCC 350 and Trichoderma viride MTCC 167 in a packed bed bioreactor was studied. Fungal mycelia preinduced with 5 g L-1 gallotannin were immobilized in calcium alginate gel (1.5%) and the resultant beads were packed in a column to a bed volume of 175 mm3. Gallotannin dissolved in distilled water was passed through the column and the eluate was recycled after adjusting pH to 6 with ammonium hydroxide (10%). Maximum hydrolysis of gallotannin was recorded by immobilized mycelia of F. solani and T. viride at 35 degrees and 45 degrees C after 175 and 60 min of residency period respectively. Optimum substrate concentration required for maximum hydrolysis was 10 g L-1 at pH 5 for both the fungi. Immobilized mycelia of A. niger and A. fischerii revealed maximum operational stability. Loss of activity after eighth run was in the order of-A. niger (no loss), A. fischerii (7.5%), F. solani (18%) and T. viride (18%). Stability in terms of retention of enzyme activity after 150 days of storage at 4 degrees C was A. niger (58%), A. fischerii (26.8%), F. solani (83%) and T. viride (85.1%).     

Petroleum-contaminated water treatment in a fluidized-bed bioreactor with immobilized Rhodococcus cells

Biotreatment of petroleum-contaminated water in a fluidized-bed bioreactor (FBB) is a relatively new and promising technology, which efficiency is strongly affected by the biocatalyst used. Our laboratory experiments involved biotreatment of the water contaminated with a synthetic petroleum mixture consisting of aliphatic and polyaromatic hydrocarbons (PAHs) using a continuous column bioreactor with recycle. Different type biocatalysts were tested, including Rhodococcus bacteria immobilized in hydrophobized carriers such as sawdust, poly(vinyl alcohol) cryogel (cryoPVA) and poly(acrylamide) cryogel (cryoPAAG). Biocatalyst abilities to oxidize petroleum hydrocarbons were evaluated using the Columbus Micro-Oxymax^® respirometer. The hydrophobized sawdust-supported biocatalyst demonstrated substantially higher metabolic activity than C₁₂-cryoPAAG-based biocatalyst due to larger number of immobilized Rhodococcus cells and, therefore, had benefits for application in FBBs. The obtained results showed that designed FBB process is successful, providing 70–100% removal of n-alkanes (C₁₀–C₁₉) and 66–70% removal of 2–3-ring PAHs from contaminated water after 2–3 weeks.     

Characterization and improvement of oxygen transfer in pilot plant external air-lift bioreactor for mycelial biomass production

The oxygen transfer dynamics in a pilot plant external air-lift bioreactor (EALB) during the cultivation of mycelial biomass were characterized with respect to hydrodynamic parameters of gas holdup (), oxygen transfer coefficient (K_La) and superficial gas velocity (U _g), and dissolved oxygen (DO). An increased flow rate of air supply was required to meet the increased oxygen demand with mycelial biomass growth. Consequently, an increase in air flow rate led to an increase in , K_La and the DO level. The enhancement of oxygen transfer rate in the cultivated broth system, however, was limited with highly increased viscosity of the mycelial broth. An increase in air flow rate from 1.25 to 2.00 v/v/m resulted in a low increment of oxygen transfer. The newly designed pilot plant EALB with two air spargers significantly improved processing reliability, aeration rate and K_La. The pilot plant EALB process, operated under a top pressure from 0 to 1.0 bars, also demonstrated a significant improvement of oxygenation efficiency by more than 20% in DO and K_La. The performance of the two sparger EALB process under top pressure demonstrated an efficient and economical aerobic system with fast mycelial growth and high biomass productivity in mycelial biomass production and wastewater treatment.     

Biological conversion of rifamycin B by live Humicola sp. cells immobilized in a dual hollow fiber bioreactor

The biological transformation from rifamycin B to rifamycin S was carried out with the live whole cells of Humicola sp., ATCC 20620, immobilized in a dual hollow fiber bioreactor (DHFBR). Humicola sp., inoculated in the DHFBR, proliferated successfully to a high density cell mass within the space between an outer silicone tubing and three inner polypropylene hollow fiber membranes. In order to control the cell growth a nitrogen deficient medium was fed. Conversion of rifamycin B continued for more than 30 d, whereas that of immobilized rifamycin B oxidase lasted only for 3 d in comparable conditions.In the DHFBR the volumetric productivity of rifamycin S was 0.65–1.03 mmol/(dm³ · h) with 60% conversion, while that in the rotating packed disk reactor was 0.27 mmol/(dm³ · h) with 40% conversion at a residence time of 0.5–1.5 h.     

Trichloroethylene degradation by immobilized restingcells ofMethylocystis sp. M in a gas-solid bioreactor

Summary Semicontinuous and continuous biodegradation of gaseous trichloroethylene (TCE) was achieved in a batch reactor and in a glass-column reactor, containing the alginate-immobilized cells of a methane-utilizing bacterium,Methylocystis sp. M. Since gaseous TCE was degraded in both reactors, it is suggested that atmospheric contamination by TCE can be prevented through the use of bioreactors.     

Design and performance of a trickle-bed bioreactor with immobilized hybridoma cells

A trickle-bed system employing inert matrices of vermiculite or polyurethane foam packed in the downcomer section of a split-flow air-lift reactor has been developed for hybridoma culture to enhance antibody productivity. This quiescent condition favoured occlusion and allowed the cells to achieve densities twelve fold greater (12.8×10⁶ cells/ml reactor for polyurethane foam) than in free cell suspension. The reactor was operated in a cyclic batch mode whereby defined volumes of medium were periodically withdrawn and replaced with equal volumes of fresh medium. The pH of the medium was used as the indicator of the feeding schedule. Glucose, lactate and ammonia concentrations reached a stationary value after 5 days. With vermiculite packing, a monoclonal antibody (MAb) concentration of 2.4 mg/l was achieved after 12 days. The MAb concentration declined then increased to a value of 1.8 mg/l. In the polyurethane foam average monoclonal antibody (MAb) concentrations reached a stationary value of 1.1 mg/l in the first 20 days and increased to a new stationary state value of 2.1 mg/l for the remainder of the production. MAb productivity in the trickle-bed reactor was 0.3 mg/l·d (polyurethane foam) and 0.18 mg/l.d (vermiculite) in comparison to 0.12 mg/l·d for free cell suspension. This trickle-bed system seems to be an attractive way of increasing MAb productivity in culture.     

Biological denitrification in a continuous-flow pilot bioreactor containing immobilized Pseudomonas butanovora cells

Pseudomonas butanovora, a novel denitrifying bacterium, was immobilized in composite beads and filled into a reactor system. The pilot bioreactor average denitrification activity was at ethanol-C:nitrate-N ratios of 3:1 and 1.5:1 0.88 and 0.54 kg NO3(-)-Nm(-3) d(-1), respectively. The denitrification was stable in spite of the relatively low hydraulic retention times of 2.47 and 3 h. The nitrate content of the influent was almost completely reduced at the first level of the bioreactor and the nitrite formed underwent reduction in the upper part of the reactor. The experimentally determined optimum ethanol-C:nitrate-N ratio was 1.41 +/- 0.41. In consequence of the aerobic conditions, the acetic acid produced by the oxygenation of ethanol was also detectable in the reactor effluent. The pH of the effluent (7.58) never exceeded the acceptable maximum (8.5). The nitrate removal efficiency of the cells was nearly 1000% at both C:N ratios, and the nitrite content of the effluent was around the prescribed limit throughout the continuous operation. This continuous-flow pilot bioreactor containing immobilized P. butanovora cells proved an efficient denitrification system with a relatively low retention time.     

Ethanol production by immobilized whole cells ofZymomonas mobilis in a continuous flow expanded bed bioreactor and a continuous flow stirred tank bioreactor

Continuous ethanol fermentation by immobilized whole cells ofZymomonas mobilis was investigated in an expanded bed bioreactor and in a continuous stirred tank reactor at glucose concentrations of 100, 150 and 200 g L^–1. The effect of different dilution rates on ethanol production by immobilized whole cells ofZymomonas mobilis was studied in both reactors. The maximum ethanol productivity attained was 21 g L^–1 h^–1 at a dilution rate of 0.36 h^–1 with 150 g glucose L^–1 in the continuous expanded bed bioreactor. The conversion of glucose to ethanol was independent of the glucose concentration in both reactors.