Assessment of fed-batch, semicontinuous, and continuous epothilone D production processes

Epothilone D is a member of a class of potent antineoplastic natural products produced by myxobacteria. Previously, we have described a fed-batch epothilone D production process in which an adsorber resin is incorporated into the bioreactor setup to capture and stabilize the product in situ, preventing its degradation within the bioreactor. The capture of epothilone D by these relatively large resin beads enables the development of continuous and semicontinuous culturing systems incorporating bead retention mechanisms to completely retain the product within the bioreactor, increasing the epothilone D product titer by almost 3-fold in both cases over a baseline fed-batch system. These product retention strategies, described here for production of the epothilones, are generally applicable to any system using adsorber resins as a method to capture product during a microbial cultivation.     

Visualising fouling of a chromatographic matrix using confocal scanning laser microscopy

Confocal scanning laser microscopy (CSLM) was used to visualise the spatial location of foulants during the fouling of Q Sepharose FF matrix in finite batch experiments and for examining the subsequent effectiveness of clean-in-place (CIP) treatments in cleaning the heavily fouled beads. Beads were severely fouled with partially clarified E. coli homogenate by contacting the beads with the foulant for contact times of 5 min, 1 or 12 h. The use of two different fluorescent dyes, PicoGreen and Cy5.5, for labelling genomic PicoGreen-labelled dsDNA and protein respectively, allowed the direct observation of the chromatographic beads. The extent of fouling was assessed by measuring the subsequent adsorption of Cy5.5-labelled BSA to the beads. Control studies established that the labelling of BSA did not affect significantly the protein properties. In the control case of contacting the unfouled matrix with Cy5.5-labelled BSA, protein was able to penetrate the entire matrix volume. After fouling, Cy5.5-labelled BSA was unable to penetrate the bead but only to bind near the bead surface where it slowly displaced PicoGreen-conjugated dsDNA, which bound only at the exterior of the beads. Labelled host cell proteins bound throughout the bead interior but considerably less at the core; suggesting that other species might have occupied that space. The gross levels of fouling achieved drastically reduced the binding capacity and maximum Cy5.5-labelled BSA uptake rate. The capacity of the resin was reduced by 2.5-fold when incubated with foulant for up to 1 h. However, when the resin was fouled for a prolonged time of 12 h a further sixfold decrease in capacity was seen. The uptake rate of Cy5.5-labelled BSA decreased with increased fouling time of the resin. Incubating the fouled beads in 1 M NaCl dissociated PicoGreen-labelled dsDNA from the bead exterior within 15 min of incubation but proved ineffective in removing all the foulant protein. Cy5.5-labelled BSA was still unable to bind beyond the outer region of the beads. A harsher CIP treatment of 1 M NaCl dissolved in 1 M NaOH was also ineffective in removing all the foulant protein but did remove PicoGreen-conjugated dsDNA within 15 min of incubation. Cy5.5-labelled BSA was able to bind throughout the bead interior after this more aggressive CIP treatment but at a lower capacity than in the case of fresh beads. The competitive adsorption of BacLight Red-labelled whole cells or cell debris and PicoGreen-conjugated dsDNA was also visualised using CSLM.     

Pilot-scale process for magnetic bead purification of antibodies directly from non-clarified CHO cell culture

High capacity magnetic protein A agarose beads, LOABeads PrtA, were used in the development of a new process for affinity purification of monoclonal antibodies (mAbs) from non-clarified CHO cell broth using a pilot-scale magnetic separator. The LOABeads had a maximum binding capacity of 65 mg/mL and an adsorption capacity of 25–42 mg IgG/mL bead in suspension for an IgG concentration of 1 to 8 g/L. Pilot-scale separation was initially tested in a mAb capture step from 26 L clarified harvest. Small-scale experiments showed that similar mAb adsorptions were obtained in cell broth containing 40 × 10⁶ cells/mL as in clarified supernatant. Two pilot-scale purification runs were then performed on non-clarified cell broth from fed-batch runs of 16 L, where a rapid mAb adsorption ≥96.6% was observed after 1 h. This process using 1 L of magnetic beads had an overall mAb yield of 86% and 16 times concentration factor. After this single protein A capture step, the mAb purity was similar to the one obtained by column chromatography, while the host cell protein content was very low, <10 ppm. Our results showed that this magnetic bead mAb purification process, using a dedicated pilot-scale separation device, was a highly efficient single step, which directly connected the culture to the downstream process without cell clarification. Purification of mAb directly from non-clarified cell broth without cell separation can provide significant savings in terms of resources, operation time, and equipment, compared to legacy procedure of cell separation followed by column chromatography step. © 2019 American Institute of Chemical Engineers Biotechnol. Prog., 35: e2775, 2019.     

Computer modeling of antibiotic fermentation with on-line product removal

The fermentation of Streptomyces griseus for the production of cycloheximide is similar to other antibiotic fermentations in that product synthesis is subject to feedback regulation and the desired product is degraded in the fermentation broth. The productivity of this fermentation can thus be dramatically increased by removing the antibiotic from the whole broth as it is produced. One means for effecting this on-line product removal is to contact the whole fermentation broth with neutral polymeric resin immobilized in hydrogel beads. The antibiotic adsorbs to the immobilized resin via hydrophobic interactions. In this work, the adsorption of the antibiotic onto the immobilized resin was characterized. A biochemical model of the fermentation was then used to describe the time profiles of biomass, substrate, and antibiotic in a fermentation system in which whole broth is circulated from the fermentor through a continuously stirred extractor containing the adsorbent beads. Various operating conditions were examined to optimize the productivity of the fermentation.     

Lactate production in an integrated process configuration: reducing cell adsorption by shielding of adsorbent

The problem of binding of microbial cells to an adsorbent matrix during in situ recovery of bioproducts from a fermentation broth has been addressed by shielding the adsorbent with a thin layer of a non-ionic polymer. Extractive bioconversion of lactic acid by integrating ion-exchange adsorption with the fermentation stage was studied. The effect of coating of the ion-exchanger with agarose on product recovery and cell adsorption was evaluated. Extractive fermentation with both uncoated and coated resin resulted in an increase in reactor productivity as compared to the normal fermentation. The free cell density in the system with agarose-coated beads was similar to that in control fermentation, but was significantly lower in the system with the uncoated ion-exchanger. Electron microscopic scanning of the bead surface after passage of the fermentation broth showed cells attached to the native adsorbent but not to the coated one.     

The horizontal movement of seeds in arable soil by different soil cultivation methods

1. To assess the impact of soil cultivation on the horizontal movement of seeds in arable soil, plastic beads and barley or triticale seeds were used as seed models. Different coloured beads were introduced in the field immediately before each of five cultivations: ploughing, two tine cultivations, harrowing and seed drilling. Beads were recovered from 20-cm soil cores divided into four 5-cm deep soil horizons.
2. After a typical cultivation sequence of five operations, beads were found up to 15 m from their source, although most beads were found within 2 m. Most beads were recovered from the surface 5 cm of the soil profile, except for those introduced onto the surface or at 20 cm depth before ploughing, which were concentrated below 10 cm.
3. Regression analysis was used to determine the pattern of bead movement by seed drilling. A novel analysis using Fast Fourier Transforms established the probability distribution functions of the remaining cultivation operations for horizontal movement. Using the final seed distributions, the effects of each cultivation were sequentially deconvoluted and the probability distribution functions smoothed. The proportions of beads moved were also calculated.
4. Ploughing and seed drilling moved seed the least distance compared with other cultivations. The mean distances moved were 0·36 m and 0·26 m, respectively. Tine cultivations moved beads 0·71 m and 1·21 m, while harrowing moved seed a mean distance of 1·58 m. Cultivation sequences based on ploughing are likely to limit seed movement in soil.
5. The Fourier deconvolution approach has potential for predicting future seed distributions and thus the spatial behaviour of weed patches within fields.     

Recovery of recombinant beta-glucosidase by expanded bed adsorption from Pichia pastoris high-cell-density culture broth

Methanol limited fed-batch cultivation was applied for production of a plant derived beta-glucosidase by Pichia pastoris. The beta-glucosidase was recovered by expanded bed adsorption chromatography applied to the whole culture broth. The new Streamline Direct HST1 adsorbent was compared with Streamline SP. Higher bead density made it possible to operate at two times higher feedstock concentration and at two times higher flow velocity. The higher binding capacity in the conductivity range 0-48 mS cm(-1) of Streamline Direct HST1 might be caused by the more complex interaction of multi-modal ligand in Streamline Direct HST1 compared to the single sulphonyl group in Streamline SP. Harsher elution condition had to be applied for dissociation of beta-glucosidase from Streamline Direct HST1 due to stronger binding interaction. The 5% dynamic binding capacity was 160 times higher for Streamline Direct HST1 compared to Streamline SP. The yield of beta-glucosidase on Streamline Direct HST1 (74%) was significantly higher than on Streamline SP (48%). Furthermore, beta-glucosidase was purified with a factor of 4.1 and concentrated with a factor of 17 on Streamline Direct HST1 while corresponding parameters were half of these values for Streamline SP. Thus, for all investigated parameters Streamline Direct HST1 was a more suitable adsorbent for recovery of recombinant beta-glucosidase from unclarified P. pastoris high-cell-density cultivation broth.     

Cell Culture conditions determine the enhancement of specific monoclonal antibody productivity of calcium alginate-entrapped S3H5/gamma2bA2 hybridoma cells

Immobilization offers several intrinsic advantages over free suspension cultures for the production of monoclonal antibodies. An important advantage of immobilization is the improved specific monoclonal antibody (MAb) productivity (q(MAb)) that can be obtained. However, there are conflicting reports in the literature on the enhancement of the q(MAb) with immobilization. The discrepancies between these reports can be attributed to the different to either the cultivation methods used for immobilized cell or to difference between the cell lines used in the various studies. We show that these differences may be attributed to the different cultivation methods used for one model hybridoma cell line. S3H5/Upsilon2bA2 hybridoma cells entrapped in different sizes of calcium alginate beads were cultivated in both T- and spinner flasks in order to determine whether cultivation methods (T- and spinner flasks) and bead size influence the q(MAb) Free-suspended cell cultures inoculated with cells recovered from alginate beads were also carried out in order to determine whether changes in the q(Mab) of the entrapped cells are reversible.The cultivation methods was found to influence significantly the q(MAb) of the entrapped cells. When the entrapped cells in 1-mn diameter beads were cultivated in T-flasks, the q(MAb) was not increased by 200% as previously observed in an entrapped cell culture using 1-mm-diameter alginate beads in spinner flasks. The q(MAb) of the entrapped cell was approximately 58% higher than that of the free-suspended cells in a control experiment. Unlike the cultivation method, the bead size in the range of 1- to 3-mm diameter did not significantly influence the q(MAb), regardless of cultivations methods. The changes in q(MAb) of an entrapped cells were reversible. When the free-suspended cells recovered from the T- and spinner flasks were sub-cultured in T- and spinner flasks enhanced q(MAb) of the entrapped cells in both cases decreased to the level of the free-suspended cell in a control experiments. Taken together, these results shows that the method of cultivation of hybridoma cells immobilized in alginate beads determines the extent of enhancement of the q(MAb). (c) 1993 John Wiley & Sons, Inc.     

Fluidized bed ion exchange for improving purification of lactic acid from fermentation

A strong anionic exchange resin was used to recover lactic acid directly from fermentation in an upflow fluidized bed column, resulting in 0.18 g lactic acid/g resin bound with a subsequent elution of 94%. When the culture broth was heated and adjusted pH to 8.0, 0.4 g lactic acid was bound per g resin, with a subsequent elution of 90%. L(+) and D(–) lactic acid isomers distribution was analyzed in the elution product resulting in an increase of L(+) isomer concentration. The resin did not alter its binding capacity after 23 cycles.     

Evaluation of a novel agarose-based synthetic ligand adsorbent for the recovery of antibodies from ovine serum

This paper evaluates a prototype agarose-based affinity adsorbent utilizing a bound synthetic ligand designed to replace Protein A as an IgG-affinity capture resin and compares its purification characteristics with four commercially available matrices for the recovery of polyclonal antibodies from crude hyperimmune ovine serum. The novel adsorbent was found to show the highest dynamic capacity (29.2 mg/mL) of all matrices under evaluation--30% higher than the other commercial adsorbents evaluated. When using a post-load caprylic acid wash, IgG yields of over 85% and purities of over 90% were achieved consistently over multiple loading cycles. To evaluate bead diffusion, inverted confocal microscopy was used to visualise fluorescent antibody binding on to individual adsorbent beads in real time. The results indicate that the binding characteristics of the prototype adsorbent are similar to those obtained with Protein G Sepharose. This study indicates that the high-capacity prototype matrix is a feasible and potentially cost-effective alternative for the direct capture of antibodies from crude ovine serum and may therefore also be applicable to the purification of other complex industrial feedstocks such as transgenic milk or monoclonal antibodies expressed using recombinant technologies.     

Maximizing the functional lifetime of Protein A resins

Protein A chromatography is currently the industry gold‐standard for monoclonal antibody and Fc‐fusion protein purification. The high cost of Protein A, however, makes resin lifetime and resin reuse an important factor for process economics. Typical resin lifetime studies performed in the industry usually examine the effect of resin re‐use on binding capacity, yield, and product quality without answering the fundamental question of what is causing the decrease in performance. A two part mechanistic study was conducted in an attempt to decouple the effect of the two possible factors (resin hydrolysis and/or degradation vs. resin fouling) on column performance over lifetime of the most commonly used alkali‐stable Protein A resins (MabSelect SuRe and MabSelect SuRe LX). The change in binding capacity as a function of sodium hydroxide concentration (rate of hydrolysis), temperature, and stabilizing additives was examined. Additionally, resin extraction studies and product cycling studies were conducted to determine cleaning effectiveness (resin fouling) of various cleaning strategies. Sodium hydroxide‐based cleaning solutions were shown to be more effective at preventing resin fouling. Conversely, cold temperature and the use of stabilizing additives in conjunction with sodium hydroxide were found to be beneficial in minimizing the rate of Protein A ligand hydrolysis. An effective and robust cleaning strategy is presented here to maximize resin lifetime and thereby the number of column cycles for future manufacturing processes. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:708–715, 2017     

Enterovirus 71 adsorption on metal ion-composite chitosan beads

In this study, we developed composite chitosan beads combining various metal ions, including Ni(2+), Cu(2+), Zn(2+), and Fe(2+), for direct adsorption of enterovirus 71 (EV71). The metal-ion species had significant effects on the adsorption capacity of beads. Among these metal ion-composite chitosan beads, Ni(2+)-chitosan beads exhibited the best adsorption capacity of EV71. Using a concentration of 0.01-M Ni(2+) was found to best provide for bead formation and EV71 adsorption. The adsorption of EV71 for Ni(2+)-chitosan beads at neutral or alkaline pH was favored. Under a competitive condition with albumin proteins, Ni(2+)-chitosan beads exhibited significant capacity of EV71 adsorption in culture media. The adsorption of EV71 on the Ni(2+)-chitosan beads was attributed to the strong binding between Ni(2+) ions chelated to the surface amino acid of EV71 capsids and Ni(2+) ions chelated on the chitosan materials. Moreover, the adsorbed EV71 retained its antigenicity and infectivity after desorption. The Ni(2+)-chitosan beads exhibit a promising application to EV71 adsorption and removal.     

Development of a polishing step using a hydrophobic interaction membrane adsorber with a PER.C6®‐derived recombinant antibody

Membrane chromatography has already proven to be a powerful alternative to polishing columns in flow‐through mode for contaminant removal. As flow‐through utilization has expanded, membrane chromatography applications have included the capturing of large molecules, including proteins such as IgGs. Such bind‐and‐elute applications imply the demand for high binding capacity and larger membrane surface areas as compared to flow‐through applications. Given these considerations, a new Sartobind Phenyl? membrane adsorber was developed for large‐scale purification of biomolecules based on hydrophobic interaction chromatography (HIC) principles. The new hydrophobic membrane adsorber combines the advantages of membrane chromatography—virtually no diffusion limitation and shorter processing time—with high binding capacity for proteins comparable to that of conventional HIC resins as well as excellent resolution. Results from these studies confirmed the capability of HIC membrane adsorber to purify therapeutic proteins with high dynamic binding capacities in the range of 20 mg‐MAb/cm³‐membrane and excellent impurity reduction. In addition the HIC phenyl membrane adsorber can operate at five‐ to ten‐fold lower residence time when compared to column chromatography. A bind/elute purification step using the HIC membrane adsorber was developed for a recombinant monoclonal antibody produced using the PER.C6® cell line. Loading and elution conditions were optimized using statistical design of experiments. Scale‐up is further discussed, and the performance of the membrane adsorber is compared to a traditional HIC resin used in column chromatography. Biotechnol. Bioeng. 2010; 105: 296–305. © 2009 Wiley Periodicals, Inc.     

The C-terminus of tubulin increases cytoplasmic dynein and kinesin processivity

In motor movement on microtubules, the anionic C-terminal of tubulin has been implicated as a significant factor. Our digital analyses of movements of cytoplasmic dynein- and kinesin-coated beads on microtubules have revealed dramatic changes when the C-terminal region (2-4-kDa fragment) of tubulin was cleaved by limited subtilisin digestion of assembled microtubules. For both motors, bead binding to microtubules was decreased threefold, bead run length was decreased over fourfold, and there was a dramatic 20-fold decrease in diffusional movements of cytoplasmic dynein beads on microtubules (even with low motor concentrations where the level of bead motile activity was linear with motor concentration). The velocity of active bead movements on microtubules was unchanged for cytoplasmic dynein and slightly decreased for kinesin. There was also a decrease in the frequency of bead movements without a change in velocity when the ionic strength was raised. However, with high ionic strength there was not a decrease in run length or any selective inhibition of the diffusional movement. The C-terminal region of tubulin increased motor run length (processivity) by inhibiting "detachment" but without affecting velocity. Because the major motor binding sites of microtubules are not on the C-terminal tail of tubulin (), we suggest that the changes are the result of the compromise of a weakly attached state that is the lowest affinity step in both motors' ATPase cycles and is not rate limiting.     

Simple fed-batch cultivation strategy for the enhanced production of a single-sugar glucuronic acid-based oligosaccharides by a cellulose-producing <Emphasis Type="Italic">Gluconacetobacter hansenii</Emphasis> strain

The production of water-soluble single-sugar glucuronic acid-based oligosaccharides (WSOS) by a cellulose producing strain Gluconacetobacter hansenii PJK was studied in a periodically recycled and fed-batch cultivations using glucose/ethanol or glucose only. Fermentations were carried out in a 2 L jar fermenter equipped with a turbine impeller with 6 flat blades. WSOS were produced constantly but the bacterial cellulose (BC) production stopped at 48 h of cultivation in a periodically recycled culture using the exhausted medium supplemented with glucose and ethanol. Tremendous quantities of WSOS were obtained in fed-batch cultivations using glucose/ethanol (35.6 g/L at 132 h of cultivation) or glucose only (86 g/L after 240 h of cultivation) as the nutritional source. However, the BC production yield under these nutritional conditions decreased significantly in comparison to previous studies about the BC production by the same strain. The overall results revealed that G. hansenii is capable of producing enormous quantities of WSOS compared to those reported previously for compounds of a related chemical nature. Moreover, the WSOS production was found to be dependent on the pH of the culture broth.     

Integration of the production and the purification processes of cutinase secreted by a recombinant Saccharomyces cerevisiae SU50 strain

By expanded bed adsorption (EBA) it was possible to simultaneously recover and purify the heterologous cutinase directly from the crude feedstock. However, it was observed that in a highly condensed and consequently economically advantageous purification process as EBA, the cultivation step highly influences the following purification step. Thus, the yeast cultivation and cutinase purification by EBA cannot be considered as independent entities, and the understanding of the interactions between them are crucial for the development of a highly cost effective overall cutinase production process. From the cultivation strategies studied, one batch, one continuous and two fed-batch cultivations, the strategy that resulted in a more economical cutinase overall production process was a fed-batch mode with a feeding in galactose. This last cultivation strategy, exhibited the highest culture cutinase activity and bioreactor productivity, being obtained 3.8-fold higher cutinase activity and 3.0-fold higher productivity that could compensate the 40% higher cultivation medium costs when compared with a fed-batch culture with a feeding on glucose and galactose. Moreover, a 3.8-fold higher effective cutinase dynamic adsorption capacity and 3.8-fold higher effective purification productivity were obtained in relation to the fed-batch culture with the feeding on glucose and galactose. The cultivation strategy with a feeding on galactose, that presented 5.6-fold higher effective purification productivity, could also compensate the 32% effective adsorption capacity obtained with a continuous cultivation broth. Furthermore, a 205-fold higher cutinase activity, 24-fold higher bioreactor productivity and 6% of the cultivation medium costs were obtained in relation to the continuous culture.     

Modeling and scale-up of the unsterile scleroglucan production process with Sclerotium rolfsii ATCC 15205

An empirical model was applied to describe the growth related formation of scleroglucan in batchwise cultivation of Sclerotium rolfsii. In this case, the level of oxygen supply controls the carbon flux into glucan, biomass, and CO₂ evolution and therefore determines the yield coefficients Y_Glucan/BDM and Y_BDM/O2. It was observed that scleroglucan formation is enhanced under microaerobic conditions. However, as the empirical model and data of actual batch cultivations show, different maxima exist for product end concentration [g/l] and volumetric productivity [g/ld] depending on the total oxygen uptake during cultivation. A sufficient bulk mixing of the highly viscous culture suspension becomes particularly important during large-scale cultivations. In addition, the scleroglucan production process proved to be shear sensitive. A correlation between the attainable molecular weight of the glucan and the stirrer tip velocity in bioreactors of different sizes is presented. For all these reasons, a scale-up of this process is very complex. Large-scale cultivations under microaerobic conditions, aiming for maximum product end concentration, were slowed down by poor bulk mixing leading to a lower carbon flux into glucan formation. On the other hand, a scale-up designed for maximum volumetric productivity using high oxygen supply was successfully conducted up to a reactor volume of 1.500 l. To minimize the loss in product quality (molecular weight of the glucan) due to high stirrer tip velocities, a mixing concept was developed employing reduced agitation combined with maximum aeration to secure a sufficient axial bulk mixing in the reactor.     

Relevance of rheological properties of gel beads for their mechanical stability in bioreactors

The mechanical stability of biocatalyst particles in bioreactors is of crucial importance for applications of immobilized-cell technology in bioconversions. The common methods for evaluation of the strength of polymer beads (mostly force-to-fracture or tensile tests) are, however, not yet proven to be relevant for the assessment of their mechanical stability in bioreactors. Therefore, we tested fracture properties of gel materials and investigated their relevance for abrasion in bioreactors. Abrasion of gel beads was assumed to be a continuous fracturing of the bead surface. At first, three rheological properties were considered: stress at fracture; strain at fracture; and the total fracture energy. If stress at fracture is the most important property, beads having a similar fracture energy, but a smaller stress at fracture, would abrade faster in a bioreactor than beads with a larger stress at fracture; if fracture energy the determining factor, beads that require less energy to fracture would abrade faster than those having a larger fracture energy for the same fracture stress. To determine this, beads of kappa-carrageenan and agar (at two different polymer concentrations) were tested for abrasion in four identical bubble columns under the same operating conditions. Agar beads were expected to abrade faster than those of carrageenan because agar had either a lower stress at fracture or a lower fracture energy. However, no correlation between fracture properties and abrasion rate was found in any of the combinations tested. Carrageenan beads abraded faster than those of agar in all combinations. Furthermore, both the stress and strain at fracture of agar and carrageenan beads decreased during the run and those of carrageenan decreased faster, suggesting that the gels are liable to fatigue in different ways. This hypothesis was confirmed by oscillating experiments in which gel samples were subjected to repeated compressions below their fracture levels. Their resistance to compression clearly decreased with the number of oscillations. Fatigue is probably related to the development of microcracks and microfracture propagation within the material. We concluded that: (a) the use of tests based on bead rupture do not provide relevant information on the mechanical stability of gel beads to abrasion; and (b) abrasion of polymer beads is likely to be related to fatigue of the gel materials. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 56: 517-529, 1997.     

Glass bead cultivation of fungi: Combining the best of liquid and agar media

Production of bioactive compounds and enzymes from filamentous fungi is highly dependent on cultivation conditions. Here we present an easy way to cultivate filamentous fungi on glass beads that allow complete control of nutrient supply. Secondary metabolite production in Fusarium graminearum and Fusarium solani cultivated on agar plates, in shaking liquid culture or on glass beads was compared. Agar plate culture and glass bead cultivation yielded comparable results while liquid culture had lower production of secondary metabolites. RNA extraction from glass beads and liquid cultures was easier than from agar plates and the quality was superior. The system allows simple control of nutrient availability throughout fungal cultivation. This combined with the ease of extraction of nucleic acids and metabolites makes the system highly suitable for the study of gene regulation in response to specific nutrient factors.     

Fluidized bed design parameters affecting novel lactic Acid downstream processing.

Lactic acid purification was directly done from fermentation utilizing a fluidized bed column refilled with a strong anionic exchange resin. The purpose of this work was to study the influence of two important design parameters, bed-diameter (D) and bed-height (H), in the lactic acid binding and elution capacity of the matrix. By changing the settled bed height from 2.5 to 5 cm for each diameter of column analyzed it was possible to obtain an 50% increase in the binding capacity of the resin in all experiments. This fact was attributed to a higher contact time between the culture broth and the anionic resin produced by the increase of back mixing and lactic acid residence time.