Tissue plasminogen activator (t-PA) production by human fibroblasts using a bioreactor with t-PA adsorption column

Production of t-PA by human embryonic lung fibroblasts, IMR-90 cells, is regulated by negative feedback control. The increase in the concentration of the extracellular t-PA lead to a reduction of the production. Therefore, we investigated the application of t-PA adsorption column to ceramic bed reactor to promote t-PA production. Amberlite XAD-8 was selected out as an adsorbent, because it is autoclavable and can adsorb 32,000 IU of t-PA per g wet gel. The t-PA adsorption column was located in the medium recirculation line to the vessel. On the other hand, medium was recirculated between the ceramic bed reactor and the vessel using another flow line. The bioreactor system with the adsorption column was about 2.5 times higher with the resulting cumulative t-PA than that without the adsorption column.     

Tissue plasminogen activator (t-PA) production by a high density culture of weakly adherent human embryonic kidney cells using a polyurethane-foam packed-bed culture system

Weakly adherent cells of the 293 line attached well to the internal surface of polyurethane foam (PUF) and grew to the high density of 6.83 × 10⁷ cells/cm³ PUF in stationary culture. The maximum productivity of tissue plasminogen activator (t-PA) was 0.158 IU/10⁶ cells per day. The productivity decreased at the stationary phase of cell growth, so we designed a PUF-plate packed-bed culture system for high density culture and continuous production of t-PA. A maximal cell density of 3.24 × 10⁷ cells/cm³ PUF and a t-PA productivity of 0.326 IU/10⁶cells per day were obtained in 25-day perfusion cultures. Although the cell density decreased to half that in PUF stationary culture, the t-PA productivity increased twofold and was maintained for 25 culture days.     

Modified CelliGen-packed bed bioreactors for hybridoma cell cultures

This study describes two packed bed bioreactor configurations which were used to culture a mouse-mouse hybridoma cell line (ATCC HB-57) which produces an IgG₁ monoclonal antibody. The first configuration consists of a packed column which is continuously perfused by recirculating oxygenated media through the column. In the second configuration, the packed bed is contained within a stationary basket which is suspended in the vessel of a CelliGen^™ bioreactor. In this configuration, recirculation of the oxygenated media is provided by the CelliGen Cell Lift impeller. Both configurations are packed with disk carriers made from a non-woven polyester fabric. During the steady-state phase of continuous operation, a cell density of 10⁸ cells per cm³ of bed volume was obtained in both bioreactor configurations. The high levels of productivity (0.5 gram MAb per 1 of packed bed per day) obtained in these systems demonstrates that the culture conditions achieved in these packed bed bioreactors are excellent for the continuous propagation of hybridomas using media which contains low levels (1 %) of serum as well as serum-free media. These packed bed bioreactors allow good control of pH, dissolved oxygen and temperature. The media flows evenly over the cells and produces very low shear forces. These systems are easy to set up and operate for prolonged periods of time. The potential for scale-up using Fibra-cel carriers is enhanced due to the low pressure drop and low mass transfer resistance, which creates high void fraction approaching 90% in the packed bed.     

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.     

Enhancement of tissue plasminogen activator production from human normal fibroblast IMR-90 cells by limitation of cell growth

Summary Tissue plasminogen activator (t-PA) production induced by proteose peptone from IMR-90 cells was investigated. Cells monolayered on plastic surfaces had a higher ability to produce t-PA per unit cell compared to those grown tri-dimensionally on ceramic pieces. Furthermore, confluent monolayers of the cells, which suffered contact inhibition and resulted in limited growth, were available for t-PA production. Repeated batch production with microcarriers, on which the cells were almost confluent monolayers similar to those in T-flasks, was performed. Utilization of the cells, which had limited serum in the growth phase, resulted in an increase in production. Moreover, dilution of the basal components of the medium at initiation of the production phase markedly promoted t-PA production. The volumetric productivity was stable for 30 days at 100 IU/cm³ per day. The cells were then mostly retained on microcarriers. Thus, an effective and scalable method of t-PA production by normal fibroblast cells was developed. Offprint requests to: S. Mitsuda     

CO2 in large-scale and high-density CHO cell perfusion culture

Productivity in a CHO perfusion culture reactor was maximized when pCO₂ was maintained in the range of 30–76 mm Hg. Higher levels of pCO₂ (> 150 mm Hg) resulted in CHO cell growth inhibition and dramatic reduction in productivity. We measured the oxygen utilization and CO₂ production rates for CHO cells in perfusion culture at 5.55×10^-17 mol cell^-1 sec^-1 and 5.36×10^-17 mol cell^-1 sec^-1 respectively. A simple method to directly measure the mass transfer coefficients for oxygen and carbon dioxide was also developed. For a 500 L bioreactor using pure oxygen sparge at 0.002 VVM from a microporous frit sparger, the overall apparent transfer rates (k_La+k_AA) for oxygen and carbon dioxide were 0.07264 min^-1 and 0.002962 min^-1 respectively. Thus, while a very low flow rate of pure oxygen microbubbles would be adequate to meet oxygen supply requirements for up to 2.1×10⁷ cells/mL, the low CO₂ removal efficiency would limit culture density to only 2.4×10⁶ cells/mL. An additional model was developed to predict the effect of bubble size on oxygen and CO₂ transfer rates. If pure oxygen is used in both the headspace and sparge, then the sparging rate can be minimized by the use of bubbles in the size range of 2–3 mm. For bubbles in this size range, the ratio of oxygen supply to carbon dioxide removal rates is matched to the ratio of metabolic oxygen utilization and carbon dioxide generation rates. Using this strategy in the 500 L reactor, we predict that dissolved oxygen and CO₂ levels can be maintained in the range to support maximum productivity (40% DO, 76 mm Hg pCO₂) for a culture at 10⁷ cells/mL, and with a minimum sparge rate of 0.006 vessel volumes per minute.A = volumetric agitated gas-liquid interfacial area at the top of the liquid, 1/mB = cell broth bleeding rate from the vessel, L/minCER = carbon dioxide evolution rate in the bioreactor, mol/min[CO₂] = dissolved CO₂ concentration in liquid, M[CO₂]^* = CO₂ concentration in equilibrium with sparger gas, M[CO₂]^** = CO₂ concentration in equilibrium with headspace gas, MCO₂(1) = dissolved carbon dioxide molecule in water[C_T] = total carbonic species concentration in bioreactor medium, M[C_T]_F = total carbonic species concentration in feed medium, MD = bioreactor diameter, mD_I = impeller diameter, mD_b = the initial delivered bubble diameter, mF = fresh medium feeding rate, L/minH_L = liquid height in the vessel, mk_A = carbon dioxide transfer coefficient at liquid surface, m/mink _infA ^supO = oxygen transfer coefficient at liquid surface, m/minNomenclature     

Kinetics of an extracellular exo-inulinase production from a 5-flourocytosine resistant mutant of Geotrichum candidum using two-factorial design

In the present study, eight different strains of Geotrichum candidum were isolated and screened for an extracellular exo-inulinase production using chemically enriched sucrose–mineral media. The isolate (Zool-3i) with a better enzyme activity (1.38 IU/ml) was subjected to induced mutagenesis using methyl methane sulphonate (MMS) and a mutant with an enzyme activity of 32.06 IU/ml was obtained. Further exposure to ethyl methane sulphonate (EMS) and ultraviolet (UV) radiations yielded a mutant exhibiting an improved activity of 39.34 IU/ml. The potential mutant was cultured overnight and plated on 5fc–YPR agar medium and thus made resistant against 5-flourocytocine. Over 50-fold enhancement in enzyme production (71.85 IU/ml) was achieved when the process parameters including incubation period (48 h), sucrose concentration (5.0 g/L), pH (6.0), inoculum size (2.0%, 16 h old) and urea (0.2%) were identified using Plackett–Burman design. On the basis of kinetic variables, notably Q_p (0.723 U/g/h), Y_p/s (2.036 U/g) and q_p (0.091 U/g cells/h), the mutant MEU-5fc-6 was found to be a hyper producer of exo-inulinase (HS, LSD 0.045, p ? 0.05).     

Gas phase H<Subscript>2</Subscript>S product recovery in a packed bed bioreactor with immobilized sulfate-reducing bacteria

An N₂ strip gas was used in a packed bed sulfate-reducing bioreactor to recover the dissolved sulfide product and improve sulfate conversion. The highest volumetric productivity obtained was 261 mol H₂S m⁻³ d⁻¹. Lowering the initial pH of the medium from 7 to 6 increased the H₂S content of the strip gas from 3.6 to 5.8 mol%. The ratio of strip gas to liquid flow rates (G/L) was found be to a suitable basis for scaling the process. Calculations indicated that modest G/L values (<10²) were required to recover the residual dissolved sulfide in a downstream stripping column.     

Improvement of the culture stability of non-anchorage-dependent animal cells grown in serum-free media through immobilization

A murine hybridoma cell line producing a monoclonal antibody against penicillin-G-amidase and a murine transfectoma cell line secreting a monovalent chimeric human/mouse Fab-antibody fragment were cultivated in three different media (serum-containing, low protein serum-free, and iron-rich protein-free) in flask cultures, stirred reactors and a fixed bed reactor. In static batch cultures in flasks both cell lines showed similar good growth in all three media.In suspension in a stirred reactor, the hybridoma cell line could be cultivated satisfactory only in serum-containing medium. In low protein serum-free medium, Pluronic F68 had to be added to protect the hybridoma cells against shear stress. But even with this supplement only batch, not chemostat mode was possible. In iron-rich protein-free medium the hybridoma cells grew also in continuous chemostat mode, but the stability of the culture was low. The transfectoma cell line did not grow in stirred reactors in any of the three media.Good results with both cell lines were obtained in fixed bed experiments, where the cells were immobilized in macroporous Siran^®-carriers. The media, which were optimized in flask cultures, could be used without any further adaptation in the fixed bed reactor. Immobilization improved the stability and reliability of cultures of non-adherent animal cells in serum-free media tremendously compared to suspension cultures in stirred reactors. The volume-specific glucose uptake rate, an, indicator of the activity of the immobilized cells, was similar in all three media. Deviations in the metabolism of immobilized and suspended cells seem to be mainly due to low oxygen concentrations within the macroporous carriers, where the cells are supplied with oxygen only by diffusion.List of symbols c substrate or product concentration mmol l^–1 - c₀ substrate or product concentration in the feed mmol l^–1 - c_Glc glucose concentration mmol l^–1 - c_Gln glutamine concentration mmol l^–1 - c_Amm ammonia concentration mmol l^–1 - c_Lac lactate concentration mmol l^–1 - c_FAB concentration of Fab# 10 antibody fragment g l^–1 - c_MAb monoclonal antibody concentration mg l^–1 - D dilution rate d^–1 - q cell-specific substrate uptake or metabolite production rate mmol cell^–1 h^–1 - q_Glc cell-specific glucose uptake rate mmol cell^–1 h^–1 - q_Gln cell-specific glutamine uptake rate mmol cell^–1 h^–1 - q_MAb cell-specific MAb production rate mg cell^–1 h^–1 - q^* volume-specific substrate uptake or metabolite production rate mmol l^–1 h^–1 - q^*FB volume-specific substrate uptake or metabolite production rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - q^*FB,Glc volume-specific glucose uptake rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - q^*FB,Gln volume-specific glutamine uptake rate related to the fixed volume mmol l_FB ^–1 h^–1 - q^*FB,MAb volume-specific MAb production rate related to the fixed volume mg l_FB ^–1 h^–1 - q^*FB,02 volume-specific oxygen uptake rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - t time h - U superficial flow velocity mm s^–1 - V medium volume in the conditioning vessel of the fixed bed reactor l - V_FB volume of the fixed bed l - x_v viable cell concentration cells ml^–1 - y_Amm,Gln yield of Ammonia from glutamine - y_Lac,Glc yield of lactate from glucose - specific growth rate h^–1 - _d specific death rate h^–1     

Enhancement of lipase production from hydrocarbons by mutation of Trichosporon fermentans

Lipase high-producing mutants with petroleum products as carbon sources were successfully induced from Trichosporon fermentans WU-C12 by ultraviolet (UV) light irradiation. In the first mutation step, one mutant strain, PU-30, derived from strain WU-C12 was selected. The productivity of extracellular lipase of PU-30 reached 58 units (U)/ml in the medium containing kerosene, being approximately twice the productivity of the parental strain WU-C12. In the second mutation step, the mutant strain 2PU-18 was induced from strain PU-30. In medium containing kerosene, gas oil and liquid paraffin, the 2PU-18 produced 70 U/ml, 62 U/ml and 60 U/ml of extracellular lipase, respectively. When various n-alkanes (C₈-C₁₈) were used as carbon sources, the parental strain WU-C12 produced more than 20 U/ml of lipase only from C₉-C₁₂ alkanes, but 2PU-18 could produce more than 50 U/ml of lipase from C₈-C₁₈ alkanes. When cultivated for 3 days in medium containing liquid paraffin, the activity ratios of extracellular lipase to total lipase and the values of extracellular lipase activity per dry-cell weight were 0.44 and 0.65 U/mg for WU-C12, and 0.62 and 1.82 U/mg for 2PU-18, respectively. These results indicate that the mutant strain 2PU-18 is superior in both total lipase productivity and permeability of lipase to the parental strain WU-C12 when petroleum products are used as carbon sources. Correspondence to: S. Usami     

里氏木霉306产t-PA固态发酵条件的研究

对基因工程菌株里氏木霉(Trichodermareesei)306生物合成组织型纤溶酶原激活剂(t-PA)的固态发酵培养基成分和发酵条件进行了研究;分析了发酵过程中t-PA的生成、总糖的消耗和菌体生长的规律。在优化的固体发酵条件下,t-PA的最大酶活是924.63IU/g干重培养基,较初始条件下提高了5倍。通过浅盘进行了放大实验,最大酶活为983.64IU/g干重培养基,t-PA合成速率为:13.66IU/g干重培养基.h,较三角瓶固态发酵最高产酶提高了6.38%,产酶速率提高了24.07%。     

Continuous acetone-butanol fermentation: a global approach for the improvement in the solvent productivity in synthetic medium

Summary The present chemostat culture studies were performed in a partial gas recycle system using Clostridium acetobutylicum ATCC 824. Initiation of chemostat cultures at two different levels of vitamins has demonstrated a more than 3 fold improvement in the solvent productivity. The production of extracellular autobacteriocin was increased markedly, when strict anaerobic conditions of the feed vessel were not maintained. When pH was regulated at 4.4, very little variation was seen in the concentration of acids. The duration of solvent production was reduced significantly when NH₄OH was replaced by NaOH for pH regulation, whereas a marked increase in the production of extracellular autobacteriocin was observed. In the optimised medium conditions, a solvent productivity of 2.09 g l^-1 h^-1 (highest ever) could be obtained in the synthetic medium.     

Production of pullulanase by free and immobilized cells of <Emphasis Type="Italic">Bacillus licheniformis</Emphasis> NRC22 in batch and continuous cultures

The production of extracellular pullulanase by Bacillus licheniformis NRC22 was investigated using different fermentation modes. In batch culture maximal enzyme activity of 18 U/ml was obtained after 24 h of growth. In continuous fermentation by the free cells, maximal reactor productivity (4.15 KU/l/h) with enzyme concentration of 14.8 U/ml and specific productivity of 334.9 U/g wet cells/h was attained at a dilution rate of 0.28/h, over a period of 25 days. B. licheniformis NRC22 cells were immobilized on Ca-alginate. The immobilization conditions with respect to matrix concentration and cell load was optimized for maximal enzyme production. In repeated batch operation, the activity of the immobilized cells was stable during the 10 cycles and the activity remained between 9.8 and 7.7 U/ml. Continuous production of pullulanase by the immobilized cells was investigated in a packed–bed reactor. Maximal reactor productivity (7.0 KU/h) with enzyme concentration of 16.8 U/ml and specific productivity of 131.64 U/g wet cells/h was attained at dilution rate of 0.42/h. The enzyme activity in the effluent started to decline gradually to the level of 8.7 U/ml after 25 days of the operation.     

Kinetics of producing pro-urokinase in perfusion cultivations

Summary Better production of pro-urokinase from human cell line was observed with 5% serum containing medium than 10% or serum free medium on Cytodex II under perfusion chemostat operations, showing 0.8×10^–5 (IU/daycell) of maximum productivity at 0.020 (l/h) of dilution rate in 5% serum medium, which corresponds to 800 IU/mL at this dilution rate. Conversion of pro-urokinase was reduced in the serum-containing media.     

Large-scale production of Erythroid Differentiation Factor (EDF) by gene-engineered Chinese hamster ovary (CHO) cells in suspension culture

From Chinese hamster ovary (CHO) cells which were producing Erythroid Differentiation Factor (EDF) in a culture medium, anchorage-independent cells, named as CHO-SPN, were produced by repeated cultivating in a suspension system. The growth time and maximum cell density of the CHO-SPN cells were 48 h and 7.8×10⁵ viable cells/ml. CHO-SPN cells accumulated 8,000 units/ml (corresponding to 4 mg/ml) of EDF in 4d. After 20 cycles of culture, CHO-SPN cells still possessed the same EDF productivity and the same growth kinetics. Furthermore, in an appropriate dissolved oxygen concentration and pH controlled culture system, the growth time and cell density became 24 h and 1×10⁶ viable cells/ml. The critical level of dissolved oxygen for cell growth was 0.015 atm. The maximum oxygen demand was 3.3×10⁻⁹ mole of O₂/ml/min.Fetal bovine serum (FBS) was indispensable for cell growth. However, a FBS-free medium (ASF201) was available for maintenance of the CHO-SPN cells, and EDF production occurred in the same medium.     

The optimization of serum-free medium for the production of the scu-PA by the addition of algal extracts

The addition of 2.8 g/ml algal extracts enhanced both scu-PA production and cell growth in a serum-free medium, compared to a conventional serum-free medium for the cultivation of recombinant CHO cells. The growth rate and scu-PA production were relatively lower in the serum-free medium than 5% serum containing medium: however, specific scu-PA production rate was higher in the serum-free medium due to the long-term period of cultivation (3.66×10^–4 vs. 2.48×10^–4 IU/cell/day). Overall scu-PA production rate was also greater in an enforced serum-free medium as 25,000 IU/day over 50 d of perfusion cultivation. The conversion ratio of scu-PA to tcu-PA was greatly reduced in the serum-free medium during perfusion cultivation (10% compared to 20% conversion in a serum containing medium).     

Determination of cell lysis and death kinetics in continuous hybridoma cultures from the measurement of lactate dehydrogenase release

The death of the hybridoma VO 208 in a continuous culture at pH 7 and 6.8 was investigated by measuring both the appearance of visible dead cells which do not exclude the trypan blue dye and the release of lactate dehydrogenase (LDH) in the culture medium. The intracellular LDH was found to be completely released either when live cells lysed or when they were transformed into visible dead cells. No significant lysis of blue dead cells could be observed at the two different pH. Using a LDH balance over the culture system, cell lysis was found negligible at pH 7, but accounted for 20% of the total cell death at pH 6.8. A methodology is proposed to evaluate the rate constants of hybridoma lysis and total death. For the investigated cell line in continuous culture, the calculated total cell death rate constant was found to increase from 0.002 h^–1 to 0.01 h^–1 when decreasing the pH from 7 to 6.8.Abbreviations D dilution rate (h^–1) - k_b specific trypan-blue dead cells appearance rate (h^–1) - k_L specific lysis rate of viable cells (h^–1) - k_d specific death rate (h-1) - LDH₀ lactate dehydrogenase activity in the feed culture medium (IU.l^–1) - LDH lactate dehydrogenase activity in the outlet culture medium (IU.l^–1) - LDH_i intracellular lactate dehydrogenase activity of viable cells (IU.10^–9 cells) - r_LDH total rate of LDH release (IU.h^–1.L^–1) - r_b transformation rate of viable cells into blue dead cells (10⁹ cells.h^–1.L^–1) - x_v viable cell concentration (10⁹ cells.l^–1) - x_b trypan-blue dead cell concentration (10⁹ cells.l^–1)     

Extracellular Location of Thermobifida fusca Cutinase Expressed in Escherichia coli BL21(DE3) without Mediation of a Signal Peptide

Cutinase is a multifunctional esterase with potential industrial applications. In the present study, a truncated version of the extracellular Thermobifida fusca cutinase without a signal peptide (referred to as cutinase^NS) was heterologously expressed in Escherichia coli BL21(DE3). The results showed that the majority of the cutinase activity was located in the culture medium. In a 3-liter fermentor, the cutinase activity in the culture medium reached 1,063.5 U/ml (2,380.8 mg/liter), and the productivity was 40.9 U/ml/h. Biochemical characterization of the purified cutinase^NS showed that it has enzymatic properties similar to those of the wild-type enzyme. In addition, E. coli cells producing inactive cutinase^NSS130A were constructed, and it was found that the majority of the inactive enzyme was located in the cytoplasm. Furthermore, T. fusca cutinase was confirmed to have hydrolytic activity toward phospholipids, an important component of the cell membrane. Compared to the cells expressing the inactive cutinase^NSS130A, the cells expressing cutinase^NS showed increased membrane permeability and irregular morphology. Based on these results, a hypothesis of “cell leakage induced by the limited phospholipid hydrolysis of cutinase^NS” was proposed to explain the underlying mechanism for the extracellular release of cutinase^NS.     

Enhancement of L-glutamate oxidase production in liquid fermentation of Streptomyces sp. by calcium addition

Summary The effect of calcium ions on production of extracellular L-glutamate oxidase (GluOx) in liquid fermentation of Streptomyces sp. N1 was investigated. By supplementing a relatively large amount of Ca²⁺ (15–40 mM) to the medium, the GluOx production was significantly enhanced, although the microbial growth was inhibited to some degree. For the first time, the highest production (i.e. 6.5 U/ml) and productivity (i.e. 0.25 U/ml/h) of GluOx as ever reported (i.e., 1.2 U/g medium after 144 h solid state fermentation and 0.59 U/ml after 96 h liquid fermentation) were achieved with addition of 30 mM Ca²⁺.     

Optimization of lactic acid production by immobilized <Emphasis Type="Italic">Lactococcus lactis</Emphasis> IO-1

Production of lactic acid from glucose by immobilized cells of Lactococcus lactis IO-1 was investigated using cells that had been immobilized by either entrapment in beads of alginate or encapsulation in microcapsules of alginate membrane. The fermentation process was optimized in shake flasks using the Taguchi method and then further assessed in a production bioreactor. The bioreactor consisted of a packed bed of immobilized cells and its operation involved recycling of the broth through the bed. Both batch and continuous modes of operation of the reactor were investigated. Microencapsulation proved to be the better method of immobilization. For microencapsulated cells at immobilized cell concentration of 5.3 g l⁻¹, the optimal production medium had the following initial concentrations of nutrients (g l⁻¹): glucose 45, yeast extract 10, beef extract 10, peptone 7.5 and calcium chloride 10 at an initial pH of 6.85. Under these conditions, at 37 °C, the volumetric productivity of lactic acid in shake flasks was 1.8 g l⁻¹ h⁻¹. Use of a packed bed of encapsulated cells with recycle of the broth through the bed, increased the volumetric productivity to 4.5 g l⁻¹ h⁻¹. The packed bed could be used in repeated batch runs to produce lactic acid.