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At least 73 records · Page 4Linked to original sources

PubMed2000

ATR-FTIR sensor development for continuous on-line monitoring of chlorinated aliphatic hydrocarbons in a fixed-bed bioreactor.

This article describes the continuous on-line monitoring of a dechlorination process by a novel attenuated total reflection-Fourier transform infrared (ATR-FTIR) sensor. This optical sensor was developed to measure noninvasively part-per-million (ppm) concentrations of trichloroethylene (TCE), tetrachloroethylene (PCE), and carbon tetrachloride (CT) in the aqueous effluent of a fixed-bed dechlorinating bioreactor, without any prior sample preparation. The sensor was based on an ATR internal reflection element (IRE) coated with an extracting hydrophobic polymer, which prevented water molecules from interacting with the infrared (IR) radiation. The selective diffusion of chlorinated compound molecules from aqueous solution into the polymer made possible their detection by the IR beam. With the exclusion of water the detection limits were lowered, and measurements in the low ppm level became possible. The best extracting polymer was polyisobutylene (PIB) in the form of a 5.8-microm thick film, which afforded a detection limit of 2, 3, and 2. 5 mg/L (ppm) for TCE, PCE, and CT, respectively. Values of the enrichment factors between the polymer coating and the water matrix of these chloro-organics were determined experimentally and were compared individually with predictions obtained from the slopes of absorbance/concentration curves for the three analytes. Before coupling the ATR-FTIR sensor to the dechlorinating bioreactor, preliminary spectra of the chlorinated compounds were acquired on a laboratory scale configuration in stop-flow and flow-through closed-loop modes. In this way, it was possible to study the behavior and direct response of the optical sensor to any arbitrary concentration change of the analytes. Subsequently, the bioreactor was monitored with the infrared sensor coupled permanently to it. The sensor tracked the progression of the analytes' spectra over time without perturbing the dechlorinating process. To calibrate the ATR-FTIR sensor, a total of 13 standard mixtures of TCE, PCE and CT at concentrations ranging from 0 to 60 ppm were selected according to a closed symmetrical experimental design derived from a 3(2) full-factorial design. The above range of concentrations chosen for calibration reflected typical values during normal bioreactor operation. Several partial least squares (PLS) calibration models were generated to resolve overlapping absorption bands. The standard error of prediction (SEP) ranged between 0.6 and 1 ppm, with a relative standard error of prediction (RSEP) between 3 and 6% for the three analytes. The accuracy of this ATR-FTIR sensor was checked against gas chromatography (GC) measurements of the chlorocompounds in the bioreactor effluents. The results demonstrate the efficiency of this new sensor for routine continuous on-line monitoring of the dechlorinating bioreactor. This strategy is promising for bioprocess control and optimization.

Biodegradation, Environmental↗

PubMed2001

Development of a novel bioreactor system for treatment of gaseous benzene.

A novel, continuous bioreactor system combining a bubble column (absorption section) and a two-phase bioreactor (degradation section) has been designed to treat a gas stream containing benzene. The bubble column contained hexadecane as an absorbent for benzene, and was systemically chosen considering physical, biological, environmental, operational, and economic factors. This solvent has infinite solubility for benzene and very low volatility. After absorbing benzene in the bubble column, the hexadecane served as the organic phase of the two-phase partitioning bioreactor, transferring benzene into the aqueous phase where it was degraded by Alcaligenes xylosoxidans Y234. The hexadecane was then continuously recirculated back to the absorber section for the removal of additional benzene. All mass transfer and biodegradation characteristics in this system were investigated prior to operation of the integrated unit, and these included: the mass transfer rate of benzene in the absorption column; the mass transfer rate of benzene from the organic phase into the aqueous phase in the two-phase bioreactor; the stripping rate of benzene out of the two-phase bioreactor, etc. All of these parameters were incorporated into model equations, which were used to investigate the effects of operating conditions on the performance of the system. Finally, two experiments were conducted to show the feasibility of this system. Based on an aqueous bioreactor volume of 1 L, when the inlet gas flow and gaseous benzene concentration were 120 L/h and 4.2 mg/L, respectively, the benzene removal efficiency was 75% at steady state. This process is believed to be very practical for the treatment of high concentrations of gaseous pollutants, and represents an alternative to the use of biofilters.

Alcaligenes↗

PubMed2001

Effects of oxygenation and flow on the viability and function of rat hepatocytes cocultured in a microchannel flat-plate bioreactor.

The goal of this study was to investigate the viability and synthetic function of rat hepatocytes cocultured with 3T3-J2 fibroblasts in a small-scale microchannel flat-plate bioreactor with and without an internal membrane oxygenator under flow. Bioreactor channel heights ranged between 85 and 500 microm and medium flow rates ranged between 0.06 and 4.18 mL/min. The results showed that the bioreactor without the oxygenator resulted in significantly decreased viability and function of hepatocytes, whereas hepatocytes in the bioreactor with internal membrane oxygenator were able to maintain their viability and function. The shear stress calculations showed that, at lower wall shear stresses (0.01 to 0.33 dyn/cm(2)), hepatocyte functions, measured as albumin and urea synthesis rates, were as much as 2.6- and 1.9-fold greater, respectively, than those at higher wall shear stresses (5 to 21 dyn/cm(2)). Stable albumin and urea synthesis rates for 10 days of perfusion were also demonstrated in the bioreactor with internal membrane oxygenator. These results are relevant in the design of hepatocyte bioreactors and the eventual scaling-up to clinical devices.

3T3 Cells↗

PubMed2006

Proof-of-concept of a novel micro-bioreactor for fast development of industrial bioprocesses.

The experimental performance of a novel micro-bioreactor envisaged for parallel screening and development of industrial bioprocesses has been tested in this work. The micro-bioreactor with an internal volume of 4.5 mL is operated under oscillatory flow mixing (OFM), where a controllable mixing and mass transfer rates are achieved under batch or continuous laminar flow conditions. Several batch fermentations with a flocculent Saccharomyces cerevisiae strain were carried out at initial glucose concentrations (S(0)) range of approximately 5-20 g/L and compared to yeast growth kinetics in a stirred tank (ST) bioreactor. Aerobic fermentations were monitored ex situ in terms of pH, DO, glucose consumption, and biomass and ethanol production (wherever applicable). An average biomass production increase of 83% was obtained in the micro-bioreactor when compared with the ST, with less 93.6% air requirements. It also corresponded to a 214% increase on biomass production when compared with growth in a shaken flask (SF) at S(0) = 20 g/L. Further anaerobic fermentations at the same initial glucose concentration ranges gave the opportunity to use state-of-the-art fiber optics technology for on-line and real-time monitoring of this bioprocess. Time profiles of biomass concentration (measured as optical density (OD)) were very similar in the ST bioreactor and in the micro-bioreactor, with a highly reproducible yeast growth in these two scale-down platforms.

Biomass↗

PubMed2000

Dechlorination of polychlorinated methanes by a sequential methanogenic-denitrifying bioreactor system.

A two-stage bioreactor has been developed to link dechlorination of halogenated methane compounds to the anaerobic processes of methanogenesis and denitrification. A digester methanogenic consortium was shown to dechlorinate chloroform (CF) and carbon tetrachloride (CT) to dichloromethane (DCM), and DCM was then mineralized by an acclimated denitrifying biological activated carbon consortium. Combining these two processes, a sequential methanogenic-denitrifying bioreactor (SMDB) system that completely degraded polychlorinated methanes including CT, CF, and DCM was developed. More than 95% of the added CT and CF was dechlorinated in the methanogenic bioreactor with methanol as the primary substrate, and the resultant DCM was biodegraded in the denitrifying bioreactor with nitrate as the electron acceptor. In the denitrifying bioreactor, the residual CF was completely removed, and the DCM removal efficiency was more than 95%. This novel bioreactor system eliminates the need for aeration and so avoids the air contamination associated with aerobic biotreatment of volatile chlorinated pollutants. This SMDB system provides an alternative to conventional biotreatment of wastewaters and other matrices contaminated with polychlorinated methanes and is, to our knowledge, the first report on such a sequential anoxic system.

Bacteria↗

PubMed2004

Bioprocess kinetics in a horizontal rotating tubular bioreactor.

A horizontal rotating tubular bioreactor (HRTB) is a plug flow bioreactor whose interior is provided with O-ring-shaped partition walls that serve as carriers for microbial biomass. During this investigation, microbial biomass was grown in suspension and on the bioreactor inner surface as a microbial biofilm with average mass that was considerably higher than suspended biomass. The dynamics of bioprocess in HRTB was studied by different combinations of process parameters (bioreactor rotation speed and mean residence time) and it was monitored by withdrawing the samples from five positions along the bioreactor. During this investigation it was also observed that mean residence time had a more pronounced effect on the bioprocess dynamics than bioreactor rotation speed. For the description of bioprocess kinetics in HRTB an unstructured kinetic model was established that defines biomass growth, product formations and substrate consumption rate by using a modified Monod (Levenspiel) model. This kinetic model defines changes in suspension and in microbial biofilm, and it shows relatively good agreement with experimental data.

Bacteria↗

PubMed2006

Long-term maintenance of human hepatocytes in oxygen-permeable membrane bioreactor.

An oxygen-permeable membrane bioreactor utilizing human hepatocytes has been tested in this study. In the bioreactor, human hepatocytes were cultured between flat-sheet gas-permeable polymeric membranes, which ensure the diffusion of O(2) and CO(2) providing a support for cell anchorage and growth and permit the online observation of the cells with an inverse microscope. This bioreactor allows a direct oxygenation of cells adhered on membranes and of the medium overlaying cells simulating in vivo sinusoidal organization. Human hepatocytes were cultured in the presence of some therapeutic molecules to assess the temporal liver-specific functions of the cells. Interleukin 6 (IL-6), which is a multifactorial proinflammatory cytokine involved in a variety of host defences and pathological processes, and diclofenac, an arylacetic non-steroidal anti-inflammatory drug, were used as therapeutic molecules. The aim of this study was to evaluate the in vitro performance of the small oxygen-permeable membrane bioreactor in the long-term maintenance and differentiation of human hepatocytes under in-vivo-like conditions. The fluid dynamics of the bioreactor were characterized before using it for human cell culture. The functional response to a step challenge in the medium of IL-6 (120 pg/ml), diclofenac (80 microm) and IL-6 and diclofenac together was investigated. The ability of hepatocytes to perform liver-specific functions in terms of urea and albumin synthesis, as well as secretion of total proteins, was maintained for 32 days. Also, the diclofenac biotransformation functions were sustained as the formation of the metabolites 4'-OH-diclofenac and 5-OH-diclofenac lactam demonstrated. This study attested the feasibility of the membrane bioreactor as an in vitro simple model system that allows human hepatocytes to be maintained in a differentiated state similar to that in vivo.

Bioreactors↗

PubMed2005

On-line analysis of CAL72 cells on two different titanium surfaces in a perfusion micro-bioreactor.

OBJECTIVES: The aim of the present experiment was to test a prototype microsensoric measuring system (micro-bioreactor) for the investigation of the biocompatibility of different titanium surfaces in a cell culture model. METHODS: Osteosarcoma cells of the cell line CAL72 were seeded onto titanium plates (10mm x 10mm x 1mm) and inserted into the culture chamber of the micro-bioreactor. Titanium plates with two different surface topographies (machined and titanium plasma-sprayed [TPS]) were used for this pilot investigation. Plastic plates served as controls. The online-sensoric device of the micro-bioreactor allowed the continuous monitoring of the metabolism of the cells and the control of the culture conditions. Over a period of 17 h changes in O(2)-consumption in the medium were measured by micro-electrodes and registered by the software of the system. The metabolic activity of the cells was calculated from the difference between the bypass and the chamber values. The cell proliferation and vitality were analyzed before and after the perfusion time in the micro-bioreactor. The cell morphology was studied using scanning electron microscopy. RESULTS: The cells on the machined surfaces showed the highest oxygen consumption after 15 h, after that it decreased. The cells on the TPS plates showed a lower oxygen consumption, which remained stable after 17 h. The highest oxygen consumption was seen with the cells on the control plastic plates. Concerning cell proliferation analysis, it could be shown that more vital CAL72 cells seeded onto TPS and plastic could be detected after the passage through the micro-bioreactor. Hence, the number of vital cells on the machined surface was reduced after the passage. SIGNIFICANCE: Within the limits of this experiment, the presented micro-bioreactor system could offer a valuable method to examine the dynamic interactions of cells and materials under defined in vitro experimental conditions. While the presented system is already successfully used in the ecological/ecotoxicological field, its routine use for investigating dental materials on a cellular level has to be evaluated.

Biocompatible Materials↗

PubMed2005

Microbial biomass production from rice straw hydrolysate in airlift bioreactors.

Rice straw is a by-product of rice production, and a great bioresource as raw biomass material for manufacturing value-adding protein for animal feedstock, which has been paid more and more attention. In the present work, utilizing rice straw hydrolysate as a substrate for microbial biomass production in 11.5L external-loop airlift bioreactors was investigated. Rice straw hydrolysate obtained through acid-hydrolyzing rice straw was used for the culture of yeast Candida arborea AS1.257. The influences of gas flow rate, initial liquid volume, hole diameter of gas sparger and numbers of sieve plates on microbial biomass production were examined. The best results in the external-loop airlift bioreactor were obtained under 9.0 L initial liquid volume, 1.1 (v/v)/min gas flow rate during culture time of 0-24 h and 1.4 (v/v)/min gas flow rate of 24-48 h at 29+/-1 degrees C. The addition of the sieve plates in the riser of the external-loop airlift bioreactor increased productivity. After 48 h, under optimized operation conditions, crude protein productivity with one sieve and two sieves were 13.6 mg/mL and 13.7 mg/mL, respectively, comparing 12.7 mg/mL without sieves in the airlift bioreactor and 11.7 mg/mL in the in the 10-L mechanically stirred tank bioreactor. It is feasible to operate the external-loop airlift bioreactors and possible to reduce the production cost for microbial biomass production from the rice straw hydrolysate.

Biomass↗

PubMed2005

Biological manganese removal from acid mine drainage in constructed wetlands and prototype bioreactors.

Mine drainage waters vary considerably in the range and concentration of heavy metals they contain. Besides iron, manganese is frequently present at elevated concentrations in waters draining both coal and metal mines. Passive treatment systems (aerobic wetlands and compost bioreactors) are designed to remove iron by biologically induced oxidation/precipitation. Manganese, however, is problematic as it does not readily form sulfidic minerals and requires elevated pH (>8) for abiotic oxidation of Mn (II) to insoluble Mn (IV). As a result, manganese removal in passive remediation systems is often less effective than removal of iron. This was found to be the case at the pilot passive treatment plant (PPTP) constructed to treat water draining the former Wheal Jane tin mine in Cornwall, UK, where effective removal of manganese occurred only in one of the three rock filter components of the composite systems over a 1-year period of monitoring. Water in the two rock filter systems where manganese removal was relatively poor was generally <pH 5, whereas it was significantly higher ( approximately pH 7) in the third (effective) system. These differences in water chemistry and manganese removal were due to variable performances in the compost bioreactors that feed the rock filter units in the composite passive systems at Wheal Jane. An alternative approach for removing soluble manganese from mine waters, using fixed bed bioreactors, was developed. Ferromanganese nodules (about 2 cm diameter), collected from an abandoned mine adit in north Wales, were used to inoculate the bioreactors (working volume ca. 700 ml). Following colonization by manganese-oxidizing microbes, the aerated bioreactor catalysed the removal of soluble manganese, via oxidation of Mn (II) and precipitation of the resultant Mn (IV) in the bioreactor, in synthetic media and mine water from the Wheal Jane PPTP. Such an approach has potential application for removing soluble Mn from mine streams and other Mn-contaminated water courses.

Bacteria↗

PubMed1997

Effects of bioreactor retention time on aerobic microbial decomposition of CELSS crop residues.

The focus of resource recovery research at the KSC-CELSS Breadboard Project has been the evaluation of microbiologically mediated biodegradation of crop residues by manipulation of bioreactor process and environmental variables. We will present results from over 3 years of studies that used laboratory- and breadboard-scale (8 and 120 L working volumes, respectively) aerobic, fed-batch, continuous stirred tank reactors (CSTR) for recovery of carbon and minerals from breadboard grown wheat and white potato residues. The paper will focus on the effects of a key process variable--bioreactor retention time--on response variables indicative of bioreactor performance. The goal is to determine the shortest retention time that is feasible for processing CELSS crop residues, thereby reducing bioreactor volume and weight requirements. Pushing the lower limits of bioreactor retention times will provide useful data for engineers who need to compare biological and physicochemical components. Bioreactor retention times were manipulated to range between 0.25 and 48 days. Results indicate that increases in retention time lead to a 4-fold increase in crop residue biodegradation, as measured by both dry weight losses and CO2 production. A similar overall trend was also observed for crop residue fiber (cellulose and hemicellulose), with a noticeable jump in cellulose degradation between the 5.3 day and 10.7 day retention times. Water-soluble organic compounds (measured as soluble TOC) were appreciably reduced by more than 4-fold at all retention times tested. Results from a study of even shorter retention times (down to 0.25 days), in progress, will also be presented.

Aerobiosis↗

PubMed2002

Urea synthesis and cyclosporin a biotransformation in a laboratory scale hepatocyte bioreactor model.

Inefficient oxygenation and build-up of waste products are inevitable in a conventional cell culture. The development of a perifusion method for isolated hepatocytes improves the process of oxygenation and helps in end-product removal. For the perifusion of cells, they must be immobilized to prepare a bioreactor model. The present work was directed to testing a hepatocyte bioreactor and maintaining tissue metabolizing activity for periods ranging from 24 to 72 h of continuous and intermittent perifusion and to test the ability of this system for cyclosporin A (CsA), biotransformation and urea synthesis as contrasted to hepatocyte in the culture. Hepatocytes were isolated, immobilized and perifused with William's E culture medium containing 1mM NH(4)Cl and CsA (20 microM). Hepatocytes in the culture were treated in the same way. CsA disappearance from the perifusion or culture media was determined by a HPLC method. Higher urea synthesis rate was achieved by cells in the continuously perifused bioreactor for 24 h compared to culture (0.5+/-0.05 mg h(-1) vs 0.33+/-0.03 mg h(-1), respectively). ALT leakage was lower in the bioreactor model (60 Ul(-1)) as compared to hepatocyte culture (125 Ul(-1)). The ability of hepatocytes in the bioreactor to metabolize CsA was very fast compared to hepatocytes in the culture during 24 h (95% vs 50%, respectively). The present data reveal the higher efficiency of hepatocytes in a bioreactor model as compared to hepatocyte culture. Further research is required in relation to better understanding and standardization of the culture conditions for immobilized and perifused hepatocytes. In addition, the cellular model described here inherits economic and ethical potentials.

Animals↗

PubMedDate not supplied

Production of extracellular protease from crude substrates with dregs in an external-loop airlift bioreactor with lower ratio of height to diameter.

Bacillus subtilis AS1.398 was cultivated in a 11.5-L total volume external-loop airlift bioreactor with a low height-to-diameter ratio of 2.9 and a riser-to-downcomer diameter ratio of 6.6 for the production of protease from crude substrates with dregs. The influence of aeration rate, liquid volume, and sparger hole diameter on protease production was investigated. An average of 8197 u/mL protease activity was obtained after a total fermentation time of 32 h in the external-loop airlift bioreactor with a liquid volume of 8.5 L, air flow rate of 1.5 vvm, and sparger hole diameter of 1.5 mm. The addition of one stainless steel sieve plate in the riser of the airlift bioreactor increased productivity of protease. After 32 h of fermentation, an average of 8718 u/mL protease activity was achieved in the external-loop airlift bioreactor with one sieve plate and an air flow rate of 1.2 vvm, liquid volume of 8.5 L, and gas sparger hole diameter of 1.5 mm. This was 9.0% higher than the typical averages of about 8000 u/mL protease activity in the mechanically stirred tank bioreactors of the enzyme factory using the same microorganism. It is possible to make a scale-up of the external-loop airlift bioreactor and feasible to operate it for production of protease from crude substrate with dregs.

Bacillus subtilis↗

PubMedDate not supplied

Computational fluid dynamics modeling of steady-state momentum and mass transport in a bioreactor for cartilage tissue engineering.

Computational fluid dynamics (CFD) models to quantify momentum and mass transport under conditions of tissue growth will aid bioreactor design for development of tissue-engineered cartilage constructs. Fluent CFD models are used to calculate flow fields, shear stresses, and oxygen profiles around nonporous constructs simulating cartilage development in our concentric cylinder bioreactor. The shear stress distribution ranges from 1.5 to 12 dyn/cm(2) across the construct surfaces exposed to fluid flow and varies little with the relative number or placement of constructs in the bioreactor. Approximately 80% of the construct surface exposed to flow experiences shear stresses between 1.5 and 4 dyn/cm(2), validating the assumption that the concentric cylinder bioreactor provides a relatively homogeneous hydrodynamic environment for construct growth. Species mass transport modeling for oxygen demonstrates that fluid-phase oxygen transport to constructs is uniform. Some O(2) depletion near the down stream edge of constructs is noted with minimum pO(2) values near the constructs of 35 mmHg (23% O(2) saturation). These values are above oxygen concentrations in cartilage in vivo, suggesting that bioreactor oxygen concentrations likely do not affect chondrocyte growth. Scale-up studies demonstrate the utility and flexibility of CFD models to design and characterize bioreactors for growth of tissue-engineered cartilage.

Bioreactors↗

PubMedDate not supplied

Microfluidic PDMS (polydimethylsiloxane) bioreactor for large-scale culture of hepatocytes.

Microfluidics could provide suitable environments for cell culture because of the larger surface-to-volume ratio and fluidic behavior similar to the environments in vivo. Such microfluidic environments are now used to investigate cell-to-cell interactions and behaviors in vitro, emulating situations observed in vivo, for example, microscale blood vessels modeled by microfluidic channels. These emulated situations cannot be realized by conventional technologies. In our previous works, microfluidic channels composed of two PDMS (poly(dimethylsiloxane)) layers were successfully used for Hep G2 cell culture. To achieve physiologically meaningful functions in vitro, a culture with a larger number of cells and higher density must be performed. This will require bioreactors with larger surface areas for cell attachment and sufficient amounts of oxygen and nutrition supply. For those purposes, we fabricated a bioreactor by stacking 10 PDMS layers together, i.e., four cell culture chambers, and a chamber dedicated to the oxygen supply inserted in the middle of the 10-stacked layers. The oxygen supply chamber is separated from the microfluidic channels for the culture medium perfusion by thin 300-microm PDMS walls. The high gas permeability of PDMS allows oxygen supply to the microfluidic channels through the thin walls. On the basis of the measurement of glucose consumption and albumin production, it is shown that cellular activity exhibits a gradual increase and saturation throughout the culture. We clearly observed that in the case of the microfluidic bioreactor for large-scale cultures, the oxygen chamber is indispensable to achieve longer and healthy cultures. In the present bioreactor, the cell density was found to be about 3-4 x 10(7) cells/cm(3), which is in the same order of magnitude as the conventional macroscale bioreactors. Consequently, by stacking single culture chambers and oxygen chambers in between, we could have a scalable method to realize the microfluidic bioreactor for large-scale cultures.

Albumins↗

PubMedDate not supplied

A novel full-scale flat membrane bioreactor utilizing porcine hepatocytes: cell viability and tissue-specific functions.

When designing an extracorporeal hybrid liver support device, special attention should be paid to providing the architectural basis for reconstructing a proper cellular microenvironment that ensures highest and prolonged functional activity of the liver cells. The common goal is to achieve high cell density culture and to design the bioreactor for full-scale primary liver cell cultures under adequate mass transfer conditions. An important aim of this study was to evaluate the biochemical performance of a flat membrane bioreactor that permits high-density hepatocyte culture and simultaneously to culture cells under sufficient oxygenation availability conditions comparable to the in vivo-like microenvironment. In such a bioreactor pig liver cells were cultured within an extracellular matrix between oxygen-permeable flat-sheet membranes. In this investigation we used a novel scaled-up prototype consisting of up to 20 modules in a parallel mode. Each module was seeded with 2 x 10(8) cells. Microscopic examination of the hepatocytes revealed morphological characteristics as found in vivo. Cell concentration increased in the first days of culture, as indicated by DNA measurements. The performance of the bioreactor was monitored for 18 days in terms of albumin synthesis, urea synthesis, ammonia elimination, and diazepam metabolism. The ability of the hepatocytes to synthesize albumin and urea increased during the first days of culture. Higher rates of albumin synthesis were obtained at day 9 and remained at a value of 1.41 pg/h/cell until day 18 of culture. The rate of urea synthesis increased from 23 ng/h/cell to 28 ng/h/cell and then remained constant. Cells eliminated ammonia at a rate of about 56 pg/h/cell, which was constant over the experimental period. Hepatocytes in the bioreactor metabolized diazepam and generated three different metabolites: nordiazepam, temazepam, and oxazepam. The production of such metabolites was sustained until 18 days of culture. These results demonstrated that the scale-up of the bioreactor was assessed, and it could be demonstrated that the device design aimed at the reconstruction of the liver-specific tissue architecture supported the expression of liver-specific functions of primary pig liver cells.

Albumins↗

PubMed1997

Retroviral transduction of peripheral blood leukocytes in a hollow-fiber bioreactor.

BACKGROUND: Peripheral blood white cells (leukocytes) (PBLs) have been used as effective targets for genetic manipulation by transduction with retroviruses in open systems. A semi-closed hollow-fiber bioreactor was tested for culturing and transducing lymphocytes. STUDY DESIGN AND METHODS: PBLs were isolated from five healthy donors, and 5 x 10(7) cells were cultured in hollow-fiber bioreactors for 4 days after stimulation with anti-CD3 in medium containing 200 units per mL of recombinant interleukin 2. Transduction with retroviral vector containing the gene for iduronate-2-sulfatase and G 418 resistance, L2SN, was performed daily on Days 4, 5, 6, and 7, and the cells were expanded for an additional 3 days. RESULTS: PBLs from three donors were harvested from the bioreactor after transduction and expansion, and 4.5 x 10(9), 7.0 x 10(9), and 2.9 x 10(9) cells were recovered, representing 90-, 136-, and 58-fold expansions. The transduction frequency of L2SN was 10, 5, and 1 percent, respectively. For additional expansion of PBLs, in two cases the bioreactor was reinoculated with 5 x 10(7) cells, which were expanded again for 16 and 8 days, respectively, yielding 1.4 x 10(9) and 3.1 x 10(9) cells, which reflected an additional 28- and 62-fold expansion of cells. PBLs from two other donors were transduced and expanded in the bioreactor, and then 0.8 mg per mL of G 418 was added to the medium in an attempt to enrich the transduced population. Although 2.5 and 10 percent of the cells were transduced, cell death and absence of expansion in the presence of G 418 resulted in final cell lots with viabilities of only 4 and 8 percent. In all cases, the harvested cells tested negative in bacterial and fungal cultures. CONCLUSION: Hollow-fiber bioreactors are an efficient and effective system for the retroviral transduction and expansion of PBLs for clinical gene therapy.

Bioreactors↗

PubMed2006

Tissue growth in a rotating bioreactor. Part II: fluid flow and nutrient transport problems.

Fluid flow and nutrient transport around a growing tissue construct within a cylindrical bioreactor of circular cross-section are considered. The bioreactor is filled with nutrient-rich culture medium, and the growing tissue construct is modelled as a cylindrical obstacle, also of circular cross-section, at a given (moving) position within the nutrient solution. The bioreactor rotates about its cylindrical axis, and its axial length is small relative to its radius (the high-aspect ratio vessel bioreactor). This small-aspect ratio means that a simple idealized model may be considered, in which (leading order) quantities are averaged across the axial direction. The leading-order fluid flow is then of Hele-Shaw type, and may be solved for explicitly. The trajectory of the tissue construct within the rotating bioreactor is determined by analysis of the various forces acting on it. Several different modes of motion are found to be possible, depending on the experimental conditions, and examples of each type of motion are presented. Additionally, we solve the problem for the nutrient transport around the tissue construct in the special case in which the construct remains fixed in the laboratory frame, and (as the cells proliferate in response to the nutrient available locally) deduce growth rates for the construct. Finally, we discuss our results in the light of possible experimental bioreactor set-ups. We note the present model's limitations, and consider how our work could be extended and improved to inform experimental protocols in future.

Algorithms↗