Production of human hematopoietic progenitors in a clinical-scale stirred suspension bioreactor

Ex vivo expanded primitive hematopoietic cells can be utilized in bone marrow transplantation therapies to treat patients suffering from various cancers and hematopoietic malignancies. A high initial cell density (10⁶ cells/mL) and the supplement of soluble factors secreted by stromal feeders in combination with growth-promoting (interleukin-3 and stem cell factor) and growth-inhibiting (macrophage-inflammatory protein-1) cytokines resulted in high, long-term expansions (17-fold over a 14-day culture period) of human hematopoietic progenitors in a stirred suspension bioreactor. This study demonstrated that a transplantable dosage of human hematopoietic progenitor cells (8.1 ± 1.3 × 10⁶ colony forming unit-granulocyte/macrophage) can be generated from approximately 10 mL of bone marrow aspirate in a 14-day culture using a 250 mL suspension bioreactor system. © Rapid Science Ltd. 1998     

Serum-free production of a chimeric E-selectin-IgG protein from 1 to 100 l scale: Repeated batch cultivation versus continuous spin filter perfusion

On inflamed endothelium the cell surface protein E-selectin isexpressed which supports the initial process of attachment –capturing and rolling of leukocytes. A recombinant CHO cell linesecreting a soluble E-selectin-IgG chimera was cultivated competitively under serum free conditions in three different bioreactor systems: a 1 l Super-Spinner, a 2 l stirred tank bioreactor equipped with a spinfilter, and a 100 l stirred tankbioreactor. In the smallest system 25.4 mg E-selectin-IgG wereproduced in 62 days using a repeated batch process whileachieving a maximal viable cell density of 3.7 × 10⁶ cells ml^-1. Using continuous perfusion mode a total amount of35.2 mg were produced with a maximal viable cell density of1.65 × 10⁷ cells ml^-1 in the 2 l bioreactor within 29 days. Large scale cultivation in a 100 l stirred tankbioreactor yielded 105.6 mg in three batches with a maximal viable cell density of 9.7 × 10⁵ cells ml^-1 within 15 days. After removal of the cells by continuous centrifugation and a depth filter clearance step, the supernatants were concentrated via ultra filtration. Purificationwas performed by affinity chromatography with rProtein A. Integrity of the E-selectin-IgG protein was checked with SDS PAGE. Its activity was verified in a cellular adhesion assay performed with HL-60 cells and a recombinant CHO cell line expressing membrane-anchored E-selectin constitutively, and E-selectin expressing HUVECs, respectively. Soluble E-selectin-IgG was used to block adhesion to these cell layerscompetitively. A concentation of 18.8 and 37.5 g ml^-1was sufficient to reduce the amount of adhering HL-60 cells to 50% on CHO and HUVEC layers, respectively.     

Azadirachtin production in stirred tank reactors by Azadirachta indica suspension culture

Successful scale-up of Azadirachta indica suspension culture for azadirachtin production was done in stirred tank bioreactor with two different impellers. The kinetics of biomass accumulation, nutrient consumption and azadirachtin production of A. indica cell suspension culture were studied in a stirred tank bioreactor equipped with centrifugal impeller and compared with similar bioreactor with a setric impeller to investigate the role of O₂ transfer efficiency of centrifugal impeller bioreactor on overall culture metabolism. The maximum cell mass for centrifugal impeller bioreactor and stirred tank bioreactor (with setric impeller) were 18.7 and 15.5 g/L (by dry cell weight) and corresponding azadirachtin concentrations were 0.071 and 0.05 g/L, respectively. Glucose and phosphate were identified as the major growth-limiting nutrients during the bioreactor cultivation. The centrifugal impeller bioreactor demonstrated less shearing and improved O₂ transfer than the stirred tank bioreactor equipped with setric impeller with respect to biomass and azadirachtin production.     

Rheology and Shear Stress of Centaurea calcitrapa Cell Suspension Cultures Grown in Bioreactor

Centaurea calcitrapa suspension cultures were grown either in Erlenmeyer flasks or in a mechanically stirred bioreactor. Its rheological behaviour, when fitted to the Oswald–de Waele model (power law), showed pseudoplastic characteristics in both cases. The flow behaviour index (n) decreased over the course of a growth cycle and the consistency index (K) increased, reached a value of 1.81 N sⁿ m⁻² run on 2 l bioreactor. Bioreactor cultivation of C. calcitrapa cells at different agitation rates (30, 60, 100 and 250 rpm), highlighted the influence of shear forces on cell viability loss (90–34%) and phenol accumulation (74–140 μg l⁻¹), due to increased stirring speeds. Analysis of these results suggests that this cell line is shear-sensitive. An empirical exponential correlation was defined between apparent viscosity and biomass concentration, under the studied conditions, giving the possibility to estimate the prevailing broth regime and to optimize bioreactor design. Revisions requested 10 October 2005; Revisions received 19 December 2005     

Obtaining and Study of Callus and Suspension Plant Cell Cultures of <Emphasis Type="Italic">Tribulus terrestris</Emphasis> L., a Producer of Steroidal Glycosides

Callus and suspension plant cell cultures of Tribulus terrestris L., a valuable medicinal plant producing steroidal glycosides, were obtained. The seeds from an American population of T. terrestris were used as explants. Regulation of the production and growth of cell cultures, as well as the biosynthetic characteristics of the cell lines, were studied. The combination of phytohormones of 2,4-D (2.0 mg/L) and BAP (1.0 mg/L) was found to be optimal for callus induction and cultivation. Suspension cell culture obtained in liquid medium of the same composition showed such high growth characteristics during prolonged cultivation (more than 2 years) as a maximum accumulation of dry biomass of 13 g/L, specific growth rate at exponential phase of 0.24 day^–1, and economical coefficient of 0.39. A semicontinuous mode of cultivation was used to grow the plant cell suspension in a lab-scale bioreactor. Screening of the steroidal glycosides in the obtained cell cultures was carried out. Steroidal glycosides were not found in the callus cultures. However, as was demonstrated by TLC and UPLC ESI MS methods, the suspension culture contained furostanol glycosides, and their amount increased during the cultivation process. These results support the hypothesis of the autoselection of cultivated cells containing compounds promoting their proliferation in vitro.     

CFD simulation coupled with population balance equations for aerated stirred bioreactors

Mammalian cells have been widely used to produce therapeutic proteins in stirred bioreactors in suspension culture. Local hydrodynamics can have a great impact on cell proliferation and protein synthesis, but there are few reports on spatial heterogeneity of nutrients, gas bubbles, and mass transfer coefficients. We have employed computational fluid dynamics (CFD) coupled with population balance equations to study local hydrodynamics in a 20 L stirred bioreactor. The flow patterns, energy dissipation rates, gas volume fraction, gas bubble size distribution and local mass transfer coefficient have been displayed throughout the whole bioreactor. Their implications for mammalian cell culture have been discussed. This study provides an insight into rational design and optimum operation conditions in a stirred bioreactor for mammalian cell cultivation.     

Bioprocess engineering characteristics of the horizontal stirred tank

Bioreactor performance studies of the recently developed horizontal stirred tank with a volume of 421 have been carried out for fermentation with Trichosporon cutaneum. Quantification on the basis of measured oxygen transfer capacity and power consumption is presented and compared with data for a conventional vertical tank bioreactor.During the experiments it has been observed that two different forms of morphology of Trichosporon, i.e. the normal yeast-form (Y) with single cells and a mycelium-form (M) with filamentous cells, are present in the horizontal stirred tank when working with the original strain (DSM 70698). After separation both forms were characterized and later on used for bioreactor performance studies in the horizontal and vertical stirred tank. Results of oxygen efficiency show the drastic effect of the morphology change on bioreactor performance. Finally different bioreactors are quantitatively compared on the basis of oxygen transfer, power consumption and productivity using the reference fermentation system Trichosporon cutaneum.List of Symbols F m³/h flow rate (volumetric) - k _La1/h volumetric transfer coefficient of OTR - M Nm torque - n 1/s rotational speed - P Nm/s power - V m³ volume - V _G1/min gas flow rate - x kg/m³ biomass concentration - ^* morphology index - ^* engineering (specific) viscosity - _app Ns/m² apparent viscosity - ₀ N/m² yield stress (Casson law) - t _1/e h measured time acc. to momentum method [17] - tEh characteristic time of electrode response - t _Gh mean residence time of gas phase Abbreviations CFR completely filled reactor - CRR cyclic ring reactor (torus) - JLR jet loop reactor - HSTR horizontal stirred tank reactor - M mycelium-form of Trichosporon cutaneum - O₂-eff O₂-efficiency - OUR O₂-uptake rate - OTR O₂-transfer rate - STR stirred tank reactor - ThLR thin layer reactor - VSTR vertical stirred tank reactor - Y yeast-form of Trichosporon cutaneum The work presented in this paper was supported by an Austrian Research Grant (FFWF, Project no. 4496)     

Enhanced Production of Human Recombinant Proteins from CHO cells Grown to High Densities in Macroporous Microcarriers

Macroporous microcarriers entrap cells in a mesh network allowing growth to high densities and protect them from high shear forces in stirred bioreactor cultures. We report the growth of Chinese hamster ovary (CHO) cells producing either recombinant human beta-interferon (β-IFN) or recombinant human tissue-plasminogen activator (t-PA) in suspension or embedded in macroporous microcarriers (Cytopore 1 or 2). The microcarriers enhanced the volumetric production of both β-IFN and t-PA by up to 2.5 fold compared to equivalent suspension cultures of CHO cells. Under each condition the cell specific productivity (Q _P) was determined as units of product/cell per day based upon immunological assays. Cells grown in Cytopore 1 microcarriers showed an increase in Q _P with increasing cell densities up to a threshold of >1 × 10⁸ cells/ml. At this point the specific productivity was 2.5 fold higher than equivalent cells grown in suspension but cell densities above this threshold did not enhance Q _P any further. A positive linear correlation (r ² = 0.93) was determined between the specific productivity of each recombinant protein and the corresponding cell density for CHO cells grown in Cytopore 2 cultures. With a cell density range of 25 × 10⁶ to 3 × 10⁸ cells/ml within the microcarriers there was a proportional increase in the specific productivity. The highest specific productivity measured from the microcarrier cultures was ×5 that of suspension cultures. The relationship between specific productivity and cell density within the microcarriers leads to higher yields of recombinant proteins in this culture system. This could be attributed to the environment within the microcarrier matrix that may influence the state of cells that could affect protein synthesis or secretion.     

Blocked ricin-conjugated T cell immunotoxins: Effect of anti-CD6-blocked ricin on normal T cell function

Summary The biological properties of an immunotoxin composed of an anti-CD6 monoclonal antibody conjugated to whole ricin, which had been modified so that the galactose-binding sites of the B chain were blocked (blocked ricin), were examined. Treatment of peripheral blood lymphocytes with anti-CD6-blocked ricin for a 24-h period prevented T cell proliferation induced by phytohemagglutinin in a dose-dependent manner with concentrations causing 50% inhibition (IC₅₀) ranging from 5 pM to 30 pM. In contrast, treatment with either blocked ricin alone or with a control immunotoxin prepared with a B-cell-lineage-restricted monoclonal antibody gave IC₅₀ values of approximately 2 nM. Although shortening the duration of the anti-CD6-blocked ricin treatment to as little as 3 h had little significant effect on the observed inhibition, T cell viability experiments demonstrated that the magnitude of immunotoxin-induced killing after a given time period is significantly higher when the target cells become activated. Thus, from the initial concentration of cells treated with anti-CD6-blocked ricin placed in culture, 40%–45% viable cells remained after 2 days yet only 3%–9% remained if phorbol ester and Ca²⁺ ionophore were added; activation of T cells after mock treatment using blocked ricin plus nonconjugated anti-CD6 demonstrated that this effect was not the result of activation alone. The toxicity of anti-CD6-blocked ricin was also measured by inhibition of PHA-induced clonogenic growth of normal T cells. Continuous treatment of the cells using anti-CD6-blocked ricin at 0.1 nM resulted in a surviving fraction of about 3.5 × 10^–3; when immunotoxin treatment was for 24 h or less, the surviving fraction was only about 10^–1. As an indication of the unique specificity of anti-CD6-blocked ricin, immunotoxin pretreatment of potential responder cells prevented the generation of allogeneic cytolytic T lymphocytes in mixed lymphocyte cultures yet had little effect on the generation of interleukin-2-induced lymphokine-activated killer cell activity. We conclude that anti-CD6-blocked ricin demonstrates a cellular specificity and potency that make it a highly promising anti-T cell reagent.     

Evaluation of a novel pneumatic bioreactor system for culture of recombinant Chinese hamster ovary cells

Single use culture systems are a tool in research and biotechnology manufacturing processes and are employed in mammalian cell-based manufacturing processes. Recently, we characterized a novel bioreactor system developed by PBS Biotech. The Pneumatic Bioreactor System? (PBS) employs the Air-wheel?, which is a mixing device similar in structure to a water wheel but is driven by the buoyant force of gas bubbles. In this study, we investigated the physical properties of the PBS system, with which we performed biological tests. In 2 L PBS, the mixing times ranged from 6 (30 rpm, 0.175 vvm) to 15 sec (10 rpm, 0.025 vvm). The k_La value reached upto 7.66/h at 0.5 vvm, even without a microsparger, though this condition is not applicable for cell cultures. Also, when a 10 L PBS equipped with a microsparger was evaluated, a k_La value of upto approximately 20/h was obtained particularly in mild cell culture conditions. We performed cultivation of Chinese hamster ovary (CHO) cells in 2 and 10 L PBS prototypes. Results from the PBS were compared with those from an Erlenmeyer flask and conventional stirred tank type bioreactor (STR). The maximum cell density of 10.6 × 106 cells/mL obtained fromthe 2 L PBSwas about 2 times higher than that from the Erlenmeyer flask (5.6 × 10⁶ cells/mL) andwas similar to the STR (9.7 × 10⁶ cells/mL) when the CHO-S cells were cultured. These results support the general suitability of the PBS system using pneumatic mixing for suspension cell cultivation as a novel single-use bioreactor system.     

Sensitization of multiple myeloma and B lymphoma lines to dexamethasone and γ-radiation-induced apoptosis by CD40 activation

We examined the effects of CD40 activation with dexamethasone (Dex) or ⁶⁰Co--irradiation on the growth of malignant B cells in vitro, using the human multiple myeloma (MM) cell line, XG2, and the B lymphoma Daudi cell line as models. Both lines are resistant to Dex and irradiation; 10^–7M Dex or 10 Gy of -irradiation induced only minimal growth arrest and apoptosis of the cells. Treatment of the cells with the agonistic anti-CD40 monoclonal antibody 5C11 partially inhibited the proliferation of the Daudi cells; XG2 underwent apoptosis. XG2 is an Interleukin-6 (IL-6)-dependent myeloma cell line and CD40 activation blocked XG2 in the G1 phase of the cell cycle, in a manner similar to the effect of IL-6 deprivation. Daudi was blocked in the G2/M phase after treatment with the agonistic CD40 mAb 5C11. Furthermore, the activation of CD40 on Daudi and XG2 enhanced their sensitivity to dexamethasone-and -irradiation -induced growth arrest and apoptosis. CD40 activation stimulated both anti-apoptotic Bcl-XL and pro-apoptotic Bax mRNA synthesis in the Daudi cell line; CD40 activation increased the Bax mRNA level but had no effect on the Bcl-XL mRNA level in the XG2 cell line. Apoptosis in both cell lines was associated with an increasing ratio of Bax-to-Bcl-XL both in mRNA and in protein levels. It is concluded that use of the anti-CD40 mAb 5C11 either by itself or in combination with chemotherapy and/or radiotherapy may have significant therapeutic potential.Z-H. Zhou and Qin Shi are equally contributed to this article.     

Somatic embryogenesis of pepper in bioreactors: a study of bioreactor type and oxygen-uptake rates

Somatic embryogenesis of pepper, Capsicum annuum var. Ace, was performed in an airlift bioreactor and a magnetically stirred hanging-stirrer-bar bioreactor, each with 1.81 working volume. All stages of embryogenesis, from growth of embryogenic suspension cultures to embryo maturation, were performed in the bioreactor as a series of drain-and-fill batches, keeping the cells and embryos in the bioreactor all the time. When two bioreactors were compared in terms of percentage embryogenesis and visually observed quality of mixing, under different rates of aeration and stirring, the performance of the magnetically stirred bioreactor was better. The effects of inoculum type and inoculum level on the percentage embryogenesis were also investigated. Under the optimum conditions, embryogenesis was 98%, with 57 embryos/ml. Oxygen-uptake rates of cultures in different stages of embryogenesis were different, the highest being in the embryogenic suspension culture and the lowest during embryo maturation.     

Continuous fermentation of a supplemented milk with immobilized Bifidobacterium infantis

Bifidobacterium infantis immobilized in -carrageenan - locust bean gum gel beads (1.0–2.0 mm diameter) was used to ferment. 10% reconstituted skim milk supplemented with 1% yeast extract in a continuous stirred tank reactor. Cell release rate from the gel beads into the milk and growth of free cells in the bioreactor allowed for a steady inoculation of the feed, with cell counts in the outflow varying from 1.0 to 2.2 × 10⁹ CFU/mL for dilution rates in the range 0,5 to 1,0 h^-1. High mechanical stability of the gel beads was observed in milk.     

Bioprocess optimization for pectinase production using <Emphasis Type="Italic">Aspergillus niger</Emphasis> in a submerged cultivation system

Background

Pectinase enzymes present a high priced category of microbial enzymes with many potential applications in various food and oil industries and an estimated market share of $ 41.4 billion by 2020.

Results

The production medium was first optimized using a statistical optimization approach to increase pectinase production. A maximal enzyme concentration of 76.35 U/mL (a 2.8-fold increase compared with the initial medium) was produced in a medium composed of (g/L): pectin, 32.22; (NH₄)₂SO₄, 4.33; K₂HPO₄, 1.36; MgSO₄.5H₂O, 0.05; KCl, 0.05; and FeSO₄.5H₂O, 0.10. The cultivations were then carried out in a 16-L stirred tank bioreactor in both batch and fed-batch modes to improve enzyme production, which is an important step for bioprocess industrialization. Controlling the pH at 5.5 during cultivation yielded a pectinase production of 109.63 U/mL, which was about 10% higher than the uncontrolled pH culture. Furthermore, fed-batch cultivation using sucrose as a feeding substrate with a rate of 2 g/L/h increased the enzyme production up to 450 U/mL after 126 h.

Conclusions

Statistical medium optimization improved volumetric pectinase productivity by about 2.8 folds. Scaling-up the production process in 16-L semi-industrial stirred tank bioreactor under controlled pH further enhanced pectinase production by about 4-folds. Finally, bioreactor fed-batch cultivation using constant carbon source feeding increased maximal volumetric enzyme production by about 16.5-folds from the initial starting conditions.

     

Cultural and physiological factors affecting expression of recombinant proteins

The variability in expression of recombinant proteins has been analyzed with regard to (a) comparison of clones from the same transfection experiment; (b) comparison of the same genetic construct in different cell lines; (c) the effect of the culture system used (free suspension, aggregate suspension, and microcarrier); and (d) physicochemical parameters in long-term (100d) culture in a macroporous fixed bed bioreactor (FBR).Differences in product expression between clones were accompanied by differences in growth rates, metabolic kinetics, and ability to grow in suspension as opposed to attached culture. The single most important factor affecting product expression when comparing constructs (for SEAP and IgG), cell lines (BHK 21 and myeloma), and culture systems was whether cells were grown in an attached or suspension mode. Thus key factors could be related to cell morphology (suspension versus monolayer), the presence of microenvironments and physiological stress to control growth rate.The relationship of key process parameters to volumetric and specific rAb productivity of the FBR was investigated in a partial factorial experiment with a rBHK cell line. The highest productivity levels are associated with a combination of the highest values tested for re-cycle (195 ml min^–1) and dilution rates (1 d^–1) and glutamine concentration (2.5 mmol l^–1), plus the lowest values for bead size (2 mm) and inoculum density (10⁷ ml^–1). Together with data from fluidised bed cultures, these results suggest that higher productivity is not primarily the result of greater cell numbers within the system but more the physicochemical definition of the system.Abbreviations FIBR fluidised bed bioreactor - FBR fixed bed reactor - STR stirred tank reactor - SEAP secreted alkaline phosphatase - rAb recombinant antibody     

Guggulsterone production in cell suspension cultures of the guggul tree, <Emphasis Type="Italic">Commiphora wightii</Emphasis>, grown in shake-flasks and bioreactors

Cell suspension cultures of Commiphora wightii, grown in modified MS medium containing 2,4-dichlorophenoxyacetic acid (0.5 mg l⁻¹) and kinetin (0.25 mg l⁻¹), produced ∼5 μg guggulsterone g⁻¹ dry wt. In a 2 l stirred tank bioreactor, the biomass was 5.5 g l⁻¹ and total guggulsterone was 36 μg l⁻¹.     

Long term and large-scale cultivation of human hepatoma Hep G2 cells in hollow fiber bioreactor

Long-term and large scale cultivation of an anchorage-dependent cell line using an industrial scale hollow fiber perfusion bioreactor is described. Hep G2 cells (a human hepatoma cell line) were cultivated in an Acysyst-P^® (Endotronic) with a total fiber surface area of 7.2 m² (6×1.2 m²) to produce Hep G2 crude conditioned medium (CCM). Pretreatment of the cellulose acetate hollow fibers with collagen enhances the attachment of the anchorage-dependent cells. We have succeeded in growing the Hep G2 cells in an antibiotics-and serum-free IMDM medium, supplemented with 50g/ml of Hep G2 CCM protein at inoculation. The Hep G2 cells replicate and secrete CCM protein in quantities comparable to those produced in DMEM containing 10% fetal calf serum (FCS). The highest CCM protein productivity during the 80-day cultivation was 1.1 g/day with a total of 30 g of protein accumulated. Hep G2 CCM (20–40 g protein/ml) was comparable to or even better than 10% FCS in supporting the growth of Molt-4 (a human T leukemia cell line) and FO (a mouse myeloma cell line) cells in vitro. The availability of this large amount of Hep G2 CCM will aid the further purification and characterization of growth factor(s) which could be used as serum substituents.     

Production of ginsenoside and polysaccharide by two-stage cultivation of Panax quinquefolium L. cells

Based on the results of carbon source consumption in cell suspension culture of Panax quinquefolium L., 30 g L⁻¹ sucrose was fed into a 5-L stirred tank bioreactor on day 16 of culture to enhance cell density and metabolite production. Using a fed-batch cultivation strategy, polysaccharide production was enhanced to 1.608 g L⁻¹, which was 1.96-fold greater than with batch cultivation. The maximum saponin yield (7.828 mg L⁻¹) was obtained on day 24 and was about 36% higher than the yields obtained using batch cultivation. In a two-stage culture process, a combined treatment with sucrose, lactoalbumin hydrolysate, and methyl jasmonate caused a significant increase in total saponin yield (31.52 mg L⁻¹) in cell cultures after 27 d. This value represents an increase of 4.03-fold compared with the total saponin yield in fed-batch cultivation. The two-stage culture mode provided the best method for the in vitro production of secondary metabolites from P. quinquefolium.     

Assessment of mass transfer and mixing in rigid lab‐scale disposable bioreactors at low power input levels

Mass transfer, mixing times and power consumption were measured in rigid disposable stirred tank bioreactors and compared to those of a traditional glass bioreactor. The volumetric mass transfer coefficient and mixing times are usually determined at high agitation speeds in combination with sparged aeration as used for single cell suspension and most bacterial cultures. In contrast, here low agitation speeds combined with headspace aeration were applied. These settings are generally used for cultivation of mammalian cells growing adherent to microcarriers. The rigid disposable vessels showed similar engineering characteristics compared to a traditional glass bioreactor. On the basis of the presented results appropriate settings for adherent cell culture, normally operated at a maximum power input level of 5 W m^?3, can be selected. Depending on the disposable bioreactor used, a stirrer speed ranging from 38 to 147 rpm will result in such a power input of 5 W m^?3. This power input will mix the fluid to a degree of 95% in 22 ± 1 s and produce a volumetric mass transfer coefficient of 0.46 ± 0.07 h^?1. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:1269–1276, 2014     

Performance of an external loop air-lift bioreactor for the production of monoclonal antibodies by immobilized hybridoma cells

Summary The performance of an external loop air-lift bioreactor was investigated by assessing the inter-relationships between various hydrodynamic properties and mass transfer. The feasibility of using this bioreactor for the production of monoclonal antibodies by mouse hybridoma cells immobilized in calcium alginate gel beads and alginate/poly-l-lysine microcapsules was also examined. When the superficial gas velocity, V _g , in the 300 ml reactor was varied from 2 to 36 cm/min, the average liquid velocity increased from 3 to 14 cm/sec, the gas hold-up rose from 0.2 to 3.0%, and the oxygen mass transfer coefficient, k _L a, increased from 2.5 to 18.1 h^-1. A minimum liquid velocity of 4 cm/s was required to maintain alginate gel beads (1000 m diameter, occupying 3% of reactor volume) in suspension. Batch culture of hybridoma cells immobilized in alginate beads followed logarithmic growth, reaching a concentration of 4×10⁷ cells/ml beads after 11 days. Significant antibody production did not occur until day 9 into the culture, reaching a value of 100 g/ml of medium at day 11. On the other hand, bioreactor studies with encapsulated hybridoma cells gave monoclonal antibody concentrations of up to 800 g/ml capsules (the antibody being retained within the semipermeable capsule) and maximum cell densities of 2×10⁸ cells/ml capsule at day 11. The volumetric productivities of the alginate gel immobilized cell system and the encapsulated cell system were 9 and 3 g antibody per ml of reactor volume per day, respectively. The main advantage of the bioreactor system is its simple design, since no mechanical input is required to vary the hydrodynamic properties.