Effects of periodic backflushing on ultrafiltration performance.

Periodic backflushing was introduced to a membrane separation process to improve the performance. Hemoglobin (M.W. = 62,500) and dextran (M.W. = 10,000) were used as model compounds. Filtration performance of an ultrafiltration membrane system (Amicon hollow fiber membrane, H1P30-43, molecular weight cutoff = 30,000) was measured in terms of apparent permeability and retention coefficient of dextran to determine the effects of backflushing frequency and duration of one cycle. An optimum frequency around 0.2 min-1 existed to give a maximum permeability while the retention of dextran decreased with increasing frequencies. The improvement in permeability by periodic backflush was more than doubled. The retention of dextran decreased as backflushing duration was increased in one cycle. With the duration of 33.75 s, the retention of dextran was less than 50% and dextran output was 1.14 g/h, which was 1.3 times the value without backflushing. Also, periodic backflush made possible the long-term filtration of yeast cells for more than 20 h.     

Comparative testing of tangential microfiltration for microbial cultures

In an attempt to extend and intensify the productive periods of bioprocesses, a self-cleaning tangential filtration device was examined. Built into a special-design bioreactor, its cell retention was evaluated for continuous-flow operation with selected examples of bacteria (Escherichia coli), yeasts (Sacharomyces cerevisiae), and filamentous fungi (Aspergillus niger). Performance characteristics such as filtration rates and cell accumulation were assessed as a function of filter rotational speed, operating pressure, cultivation time, and microfilter type (i.e., membrane or porous metallic). The highest flux of cell-free filtrate for each culture type was achieved using a 0.45-micron membrane-covered microfilter. While the respective yeast (S. cerevisiae) and bacterial (E. coli) cell concentrations were enhanced by as much as 16- and 8-fold over the batch growth levels, the representative A. niger fungal cultivation was less satisfactory because of progressively declining filtration rates limited by hydraulically resistant layers of microbial surface growth quite resistant to in situ filter backflushing with gas. Maximum steady-state flux was independent of operating pressure, yet was enhanced at rotational speeds up to about 800 rpm. Higher speeds offered no further improvements. The overall fermentation process was limited by the moderate levels of attainable flux which restricted the feed and dilution rates. The maximum attainable stabilized fluxes were 26-40 L/m(2) x h.     

Crossflow filtration of yeast broth cultivated in molasses

A broth of yeast cells cultivated in molasses was crossfiltered with a thin-channel module. The permeation flux gradually decreased at a constant cell concentration. The flux was much lower than that obtained for yeast broth cultivated in yeast extract, polypeptone, and dextrose (YPD) medium during the filtration. The flux did not depend on the membrane pore size (0.45 to 5 mum). The steady-state flux was one-twentieth that calculated for a cake filtration mode from the amount of cake per unit filtration area and the specific resistance of the cake measured in a dead-end filtration apparatus. The lower flux was due to small particles (most of which were less than 1 mum in diameter) in the molasses. The mehanism of crossflow filtration of broths of yeast cells cultivated in molasses was clarified by analysis of the change in flux with time and observations with scanning electron microscopy. At the initial stage of crossflow filtration the yeast cells and particles from the molasses were deposited on the membrane to form the molasses were deposited on the membrane to form a cake in a similar way to dead-end filtration. After the deposition of cells onto the membrane ceased, the fine particles from molasses formed a thin layer, which had higher resistance than the cake formed next to the membrane. The backwashing method was effective to increase the flux. The flux increased low when the pore size was 0.45 to 0.08 mum, but using larger pores of 3 to 5 mum it returned almost to the bases line. (c) 1994 John Wiley & Sons, Inc.     

Factors affecting membrane fouling in filtration of Saccharomyces cerevisiae in an internal ceramic filter bioreactor

Filtration of ethanol fermentation medium and broth by using symmetric and asymmetric ceramic membranes has been studied in an internal filter bioreactor. Factors studied included membrane structure and pore size, medium sterilization, and concentrations of glucose, yeast extract in the medium, yeast cell and protein in broth. The aim was to determine the main factors responsible for the decline in filtration performance during ethanol fermentation by Saccharomyces cerevisiae. Flux index (Fi) of a new concept has been developed to evaluate the degree of flux decline during the membrane fouling process. Fi was defined as the ratio of the membrane flux at certain filtration time (t?=?t) to the initial (t?=??0) flux of pure water, not the initial (t?=?+0) flux of the test fluid. Flux with sterilized medium was approximately two-fold higher than that with unsterilized medium although the reason could not be explained clearly. Glucose, interaction between glucose and yeast extract, yeast cells, and proteins in fermentation broth were found to play an important part in membrane fouling. Fi of the symmetric membrane decreased to a less extent than that of the asymmetric membrane with increasing glucose concentration. But, the result with various yeast cell concentrations turned out to be contrary. Fouling was more serious for asymmetric membrane during the filtration of fermentation supernatant. This was thought to be due to different fouling mechanisms for the two types of membrane.     

Osmotic mass transfer in the yeast Saccharomyces cerevisiae.

This paper reviews the passive mechanisms involved in the response of a yeast to changes in medium concentration and osmotic pressure. The results presented here were collected in our laboratory during the last decade and are experimentally based on the measurement of cell volume variations in response to changes in the medium composition. In the presence of isoosmotic concentration gradients of solutes between intracellular and extracellular media, mass transfers were found to be governed by the diffusion rate of the solutes through the cell membrane and were achieved within a few seconds. In the presence of osmotic gradients, mass transfers mainly consisting in a water flow were found to be rate limited by the mixing systems used to generate a change in the medium osmotic pressure. The use of ultra-rapid mixing systems allowed us to show that yeast cells respond to osmotic upshifts within a few milliseconds and to determine a very high hydraulic permeability for yeast membrane (Lp>6.10(-11) m x sec)-1) x Pa(-1)). This value suggested that yeast membrane may contain facilitators for water transfers between intra and extracellular media, i.e. aquaporins. Cell volume variation in response to osmotic gradients was only observed for osmotic gradients that exceeded the cell turgor pressure and the maximum cell volume decrease, observed during an hyperosmotic stress, corresponded to 60% of the initial yeast volume. These results showed that yeast membrane is highly permeable to water and that an important fraction of the intracellular content was rapidly transferred between intracellular and extracellular media in order to restore water balance after hyperosmotic stresses. Mechanisms implied in cell death resulting from these stresses are then discussed.     

Microfiltration cell-recycle pilot system for continuous thermoanaerobic production of exo-beta-amylase

A microfiltration cell-recycle pilot-scale system was developed comprised of a conventional continuous-flow fermentor connected to an in situ steam-sterilizable cross-flow ceramic filter with a backflushing device. A microcomputer was used to control filtration pressure, tangential flow velocity, and backflushing. Performance of the system was tested with the anaerobic production of thermostable extracellular beta-amylase at 60 degrees C by Clostridium thermosulfurogenes on maltose or malto-dextrin media. Filtration rates during continuous cultivation were between 20 and 60 L/m(2)/h. The maltodextrin and cell debris occurring at high retentate flow rates or filtration pressures impaired the performance of the filter. Backflushing initially improved the permeate flux to 42% in a maltose medium and to 10% in a maltodextrin medium, but the effect diminished with time. The productivity of beta-amylase (as much as 48 U/mL/h) and concentration of biomass (as much as 14 g/L) were increased 11- and 12-fold, respectively, if compared to values obtained in a chemostat. The concentration of beta-amylase rose to 220 U/mL in the reactor, which was 5.5-fold more than under comparable conditions in a chemostat.     

Microfiltration of recombinant yeast cells using a rotating disk dynamic filtration system

To develop a highly efficient cell harvest step under time constraint, a novel rotating disk dynamic filtration system was studied on the laboratory scale (0.147-ft.(2) nylon membrane) for concentrating recombinant yeast cells containing an intracellular product. The existing cross-flow microfiltration method yielded pseudo-steady state flux values below 25 LMH (L/m(2). h) even at low membrane loadings (10 L/ft.(2)). By creating high shear rates (up to 120,000(-1)) on the membrane surface using a rotating solid disk, this dynamic filter has demonstrated dramatically improved performance, presumably due to minimal cake buildup and reduced membrane fouling. Among the many factors investigated, disk rotating speed, which determines shear rates and flow patterns, was found to be the most important adjustable parameter. Our experimental results have shown that the flux increases with disk rotating speed, increases with transmembrane pressure at higher cell concentrations, and can be sustained at high levels under constant flux mode. At a certain membrane loading level, there was a critical speed below which it behaved similarly to a flat sheet system with equivalent shear. Average flux greater than 200 LMH has been demonstrated at 37-L/ft.(2) loading at maximum speed to complete sixfold concentration and 15-volume diafiltration for less than 100 min. An order of magnitude improvement over the crossflow microfiltration control was projected for large scale production. This superior performance, however, would be achieved at the expense of additional power input and heat dissipation, especially when cell concentration reaches above 80 g dry cell weight (DCW)/L. Although a positive linear relationship between power input and dynamic flux at a certain concentration factor has been established, high cell density associated with high viscosity impacted adversely on effective average shear rates and, eventually, severe membrane fouling, rather than cake formation, would limit the performance of this novel system. (c) 1995 John Wiley & Sons, Inc.     

Microfiltration of yeast suspensions with self-cleaning spiral vortices: possibilities for a new membrane module design

A novel method of producing controlled vortices was used to reduce both concentration polarization and membrane fouling during microfiltration of Saccharomyces cerevisiae broth suspensions. The method involves flow around a curved channel at a sufficient rate so as to produce centrifugal instabilities (called Dean vortices). These vortices depolarize the build-up of suspended particles such as yeast cells at the membrane-solution interface and allow for increased membrane permeation rates. Various operating conditions under which such vortices effectively reduced cake build-up of suspended particles such as yeast cells at the membrane-solution interface and allow for increased membrane permeation rates. Various operating conditions under which such vortices effectively reduced cake build-up during microfiltration of 0 to 0.55 dry wt% yeast broth were investigated. Flux improvements of over 60% for 0.25 dry wt% yeast broth for flow with over that without Dean vortices were observed. This beneficial effect increased with increasing retentate flow rate and increasing transmembrane pressure and decreased with increasing concentration of suspended matter. Similar behavior was observed whether the cells were viable of killed. the improvement in flux in the presence over that in the absence of vortices correlated well with centrifugal force or azimuthal velocity squared. The relative cake resistances increased with reservoir yeast concentration. These values with vortices increased from 62% to 75% of that without vortices with increasing yeast concentration. The ratio of the cake thicknesses in the limiting case (at high feed concentration) was 3.25. These results suggest that self-cleaning spiral vortices could be effective in maintaining good and steady microfiltration performance with cell suspensions other than those tested. (c) 1995 John Wiley & Sons, Inc.     

Yeast suspension filtration: flux enhancement using an upward gas/liquid slug flow-application to continuous alcoholic fermentation with cell recycle

This study deals with the use of an upward gas/liquid slug flow to reduce tubular mineral membrane fouling. The injection of air into the feedstream is designed to create hydrodynamic conditions that destabilize the cake layer over the membrane surface inside the filtration module complex. Experimental study was carried out by filtering a biological suspension (yeast) through different tubular mineral membranes. The effects of operating parameters, including the nature of the membrane, liquid and gas flowrates, and transmembrane pressure, were examined. When external fouling was the main limiting phenomenon, flux enhancements of a factor of three could be achieved with gas sparging compared with single liquid phase crossflow filtration. The economic benefits of this unsteady technique have also been examined. To investigate the possibility of long-term operation of the two-phase flow principle, dense cell perfusion cultures of Saccharomyces cerevisiae were carried out in a fermentor coupled with an ultrafiltration module. The air injection allowed a high and stable flux to be maintained over 100 h of fermentation, with a final cell concentration of 150 g dry weight/L. At equal biomass level, a twofold gain in flux could be attained compared with classical steady crossflow filtration at half the cost.     

Time-resolved measurements of intracellular ATP in the yeast Saccharomyces cerevisiae using a new type of nanobiosensor

Adenosine 5'-triphosphate is a universal molecule in all living cells, where it functions in bioenergetics and cell signaling. To understand how the concentration of ATP is regulated by cell metabolism and in turn how it regulates the activities of enzymes in the cell it would be beneficial if we could measure ATP concentration in the intact cell in real time. Using a novel aptamer-based ATP nanosensor, which can readily monitor intracellular ATP in eukaryotic cells with a time resolution of seconds, we have performed the first on-line measurements of the intracellular concentration of ATP in the yeast Saccharomyces cerevisiae. These ATP measurements show that the ATP concentration in the yeast cell is not stationary. In addition to an oscillating ATP concentration, we also observe that the concentration is high in the starved cells and starts to decrease when glycolysis is induced. The decrease in ATP concentration is shown to be caused by the activity of membrane-bound ATPases such as the mitochondrial F(0)F(1) ATPase-hydrolyzing ATP and the plasma membrane ATPase (PMA1). The activity of these two ATPases are under strict control by the glucose concentration in the cell. Finally, the measurements of intracellular ATP suggest that 2-deoxyglucose (2-DG) may have more complex function than just a catabolic block. Surprisingly, addition of 2-DG induces only a moderate decline in ATP. Furthermore, our results suggest that 2-DG may inhibit the activation of PMA1 after addition of glucose.     

Membrane fouling by cell-protein mixtures: in situ characterisation using multi-photon microscopy

Fouling of the membrane by cell and protein mixtures can result in severe flux declines, leading to the eventual need to clean or replace the membrane. In this study multi-photon microscopy, a fluorescence-based technique is used to 3-D image in situ the fouling of microfiltration membranes by suspensions containing combinations of washed yeast, bovine serum albumin (BSA) and ovalbumin. Appropriate fluorescent labelling allows the three foulant species to be clearly identified. Images correlate well with filtration data and clearly show the cake of yeast cells capturing protein aggregates. The proteins exhibited very different filtration behaviour. When filtering washed yeast together with ovalbumin and/or a 50:50 mixture by mass of BSA and ovalbumin, the ovalbumin fouling dominates the system. Capture of aggregates by the cake did not reduce fouling of the membrane by the protein and increased the resistance of the cake. For mixtures of BSA and washed yeast, the presence of a cake of yeast cells did reduce fouling of the membrane by the protein, however, the extra resistance due to the cake resulted in a flux lower than that when filtering BSA alone.     

Separation of lactic acid-producing bacteria from fermentation broth using a ceramic microfiltration membrane with constant permeate flow

The influence of several operating parameters on the critical flux in the separation of lactic acid-producing bacteria from fermentation broth was studied using a ceramic microfiltration membrane equipped with a permeate pump. The operating parameters studied were crossflow velocity over the membrane, bacterial cell concentration, protein concentration, and pH. The influence of the isoelectric point (IEP) of the membrane was also investigated. In the interval studied (5.3-10.8 m/s), the crossflow velocity had a marked effect on the critical flux. When the crossflow velocity was increased the critical flux also increased. The bacterial cells were retained by the membrane and the concentration of bacterial cells did not affect the critical flux in the interval studied (1.1-3.1 g/L). The critical flux decreased when the protein concentration was increased. It was found that the protein was adsorbed on the membrane surface and protein retention occurred even though the conditions were such that no filter cake was present on the membrane surface. When the pH of the medium was lowered from 6 to 5 (and then further to 4) the critical flux decreased from 76 L/m(2)h to zero at both pH 5 and pH 4. This was found to be due to the fact that the lowering in pH had affected the physiology of the bacterial cells so that the bacteria tended to adhere to the membrane and to each other. The critical flux, for wheat flour hydrolysate without particles, was much lower (28 L/m(2)h) when using a membrane with an IEP of 5.5 than the critical flux of a membrane with an IEP at pH 7 (96 L/m(2)h). This was found to be due to an increased affinity of the bacteria for the membrane with the lower IEP.     

The Mode of Action of Toxic Protein in Wheat and Barley on Brewing Yeast

The mode of action of the toxic protein isolated from wheat on brewing yeast was investigated, and the following results were obtained: (1) The toxin inhibits respiration and fermentation of the yeast, and causes death of the cell in a few min (6 min) at a concentration of 4 ppm. (2) At a lower concentration (0.4 ppm), the toxin inhibits incorporation of sugars without causing death of the cells. (3) Potassium ion, phosphate ion, protein and nucleotides leak from the cell upon treatment with toxin at a lower concentration (0.4 ppm). (4) A directly proportional relationship exists between the lowest lethal concentration of the toxin and the yeast cell population. (5) The toxin is adsorbed onto the cell wall and cell membrane.

According to these results, the toxin seems to react with functional site(s) of the cell membrane causing changes in the permeability of the membrane and resulting in cell death.     

Factors affecting the performance of crossflow filtration of yeast cell suspension

Factors affecting the performance of crossflow filtration were investigated with a thin-channel module and yeast cells. In crossflow filtration of Saccharomyces cerevisiae cells cultivated with YPD medium (Yeast extract, polypeptone, and dextrose) and suspended in saline, a steady state was attained within several minutes when the cell concentration was low and the circulation flow rate was high. The steady-state flux and the change in flux during the initial unsteady state were explained well by conventional filtration theory, with the amount of cake deposited and the mean specific resistance to the cake measured in a dead-end filtration apparatus used in calculation. When the circulation flow rate was lower than a critical value, a part of the channel of the crossflow filtration module was plugged with cell cake, and thus the steady-state flux was low. In crossflow filtration of suspensions of commercially available baker's yeast, the flux gradually decreased, and the flux after 8 h of filtration was lower than the value calculated by filtration theory. Fine particles contaminating the baker's yeast was responsible for the decrease. A similar phenomenon was responsible for the decrease. A similar phenomenon was observed in crossflow filtration of a broth of S. cerevisiae cells cultivated in molasses medium, which also contains such particles, had no effect of the permeation flux during crossflow filtration. (c) 1993 John Wiley & Sons, Inc.     

Separation of yeast by cross-flow filtration with backwashing

The following results were obtained at the separation of yeast by cross-flow filtration from fermentation broth or yeast suspensions with or without backwashing by the filtrate, using micro-porous membranes: 1) the first stage of the filtration process was described by the standard blocking filtration model, 2) the mean filtration flux in one filtration cycle was kept almost constant for at least 3 h by backwashing, 3) the mean filtration flux with backwashing was roughly estimated from the results of filtration without backwashing, and 4) the mean filtration flux at certain yeast concentration in concentrating the yeast was not so much affected by the previous concentration path, and almost agreed that in the filtration of a constant concentration at the same concentration.     

Long-Term Continuous Cultivation of Clostridium beijerinckii in a Two-Stage Chemostat with On-Line Solvent Removal

A two-stage continuous cultivation experiment with Clostridium beijerinckii NRRL B592 is described. This strain maintained its ability to produce neutral solvents (acetone, n-butanol, and ethanol) at an overall dilution rate of 0.13 h(sup-1) and achieved an average overall solvent concentration of 9.27 g/liter and an overall solvent productivity of 1.24 g/liter/h for more than 100 overall retention times. The experiment was performed without pH control on a semisynthetic medium containing yeast extract, and product inhibition was the limiting factor. Solid carrier material was present in both stages, and the solvent productivity in both stages was similar. A membrane evaporation module integrated into the recirculation loop of a second-stage bioreactor after 2,166 h increased solvent productivity and improved the yield of solvents by about 40%. The membrane reduced the concentration of solvents, which would otherwise inhibit the fermentation. Additionally, the integrated membrane evaporation dampened metabolic oscillations, which are characteristic of continuous cultivation of clostridia. It was also demonstrated that a moderate concentration buildup (approximately 30% of bioreactor inflow) caused by water flux through the membrane caused no detrimental effects to the bacterial cells. However, much higher water fluxes through the membrane, associated with a much more dramatic increase in the concentration of salts in the medium, did appear to favor cell degeneration.     

Osmotic regulation of Rab-mediated organelle docking

Osmotic gradients across organelle and plasma membranes modulate the rates of membrane fission and fusion; sufficiently large gradients can cause membrane rupture [1-6]. Hypotonic gradients applied to living yeast cells trigger prompt (within seconds) swelling and fusion of Saccharomyces cerevisiae vacuoles, whereas hypertonic gradients cause vacuoles to fragment on a slower time scale [7-11]. Here, we analyze the influence of osmotic strength on homotypic fusion of isolated yeast vacuoles. Consistent with previously reported in vivo results, we find that decreases in osmolyte concentration increase the rate and extent of vacuole fusion in vitro, whereas increases in osmolyte concentration prevent fusion. Unexpectedly, our results reveal that osmolytes regulate fusion by inhibiting early Rab-dependent docking or predocking events, not late events. Our experiments reveal an organelle-autonomous pathway that may control organelle surface-to-volume ratio, size, and copy number: Decreasing the osmolyte concentration in the cytoplasmic compartment accelerates Rab-mediated docking and fusion. By altering the relationship between the organelle surface and its enclosed volume, fusion in turn reduces the risk of membrane rupture.     

Hydraulic resistance and fouling of microfilters by Candida utilis in fermentation broth

The hydraulic resistance and membrane fouling effects of Candida utilis in fermentation broth were investigated using Millipore PVDF 0.22-mum membranes (GVWP and GVHP) in a stirred-cell system at 50 kPa and 700 rpm. With the various components of broth, spent medium, which contains colloidal particles and macromolecules having sizes (0.32 to 2.67 mum) comparable with the membrane pores (actual range 0.26 to 0.63 mum), was found to be the major contributing factor to the membrane fouling by broth through pore plugging. This led the spent medium to exhibit the highest hydraulic resistance (R(sm) of 5.8E + 12 m(-1)) and percentage flux loss (81.0%) when compared with either intact cells alone in buffer or to whole broth. Intact cells appeared to physically block and protect the pores without significant adhesion, because of the relatively hydrophilic nature of their cell walls (hydrophobicity of 5.9% at hour 36), resulting in the lowest hydraulic resistance (Rsbc of 7.5E + 11m(-1)) and percentage flux loss (19.3%).However, the hydraulic resistance and percentage flux loss of broth increased as cells aged. This was attributed to the increase in particle loading (intact cells by 15.37%, released cell contents and cell fragments) and in the hydrophobicity of cell walls. Autoclaved broth, lysed broth and aged broth, which contained a larger portion of colloidal particles and released cell contents caused a more pronounced fouling effect. This was revealed by the absence of flux recovery after depressurization with continuous stirring, even when a hydrophilic membrane was used. Furthermore, the hydrophobicity of C. utilis was found to increase with yeast extract present in medium, and use of hydrophobic membranes helped enhance the fouling effect. Overall, the degree of irreversible membrane fouling could be revealed by the value of R(sm)/R(t') and the hydraulic resistance, which resulted from concentration polarrzation, could be revealed by the value of R(c)/R(t') where R(t) = R(m) + R(sm) + R(c') and R(m) is the clean membrane resistance. (c) 1995 John Wiley & Sons, Inc.     

Membrane transport of anandamide through resealed human red blood cell membranes

The use of resealed red blood cell membranes (ghosts) allows the study of the transport of a compound in a nonmetabolizing system with a biological membrane. Transmembrane movements of anandamide (N-arachidonoylethanolamine, arachidonoylethanolamide) have been studied by exchange efflux experiments at 0 degrees C and pH 7.3 with albumin-free and albumin-filled human red blood cell ghosts. The efflux kinetics is biexponential and is analyzed in terms of compartment models. The distribution of anandamide on the membrane inner to outer leaflet pools is determined to be 0.275 +/- 0.023, and the rate constant of unidirectional flux from inside to outside is 0.361 +/- 0.023 s(-1). The rate constant of unidirectional flux from the membrane to BSA in the medium ([BSA]o) increases with the square root of [BSA]o in accordance with the theory of an unstirred layer around ghosts. Anandamide passed through the red blood cell membrane very rapidly, within seconds. At a molar ratio of anandamide to BSA of <1, membrane binding of anandamide increases with increasing temperatures between 0 degrees C and 37 degrees C, and the equilibrium dissociation constants are in the nanomolar range. The nature of membrane binding and the mechanism of membrane translocation are discussed.     

Cell retention culture with an internal filter module: continuous ethanol fermentation

A new internal filter feedback system with a stainless steel filter was introduced and its application for continuous ethanol fermentation was investigated. The filter performance was highly influenced by agitation speed and yeast concentration. Retention coefficient with a filter of 2 mum pore size was found more than 97.5%, and the filter was suitable for yeast separation. Maximum yeast concentration was 157 g/L and the best operable cell concentration was between 90 and 150 g/L. Which was similar to that obtained in the external membrane cell recycle culture. The cell concentration in the fermentor was maintained by manipulation of dilution rate and bleed ratio with the growth rate. The internal filter feedback system was successfully operated for more than 10 days. This study shows that the internal filter feedback system with a stainless steel filter can be used high-density cell culture and ethanol fermentation. Furthermore, it can be scaled up more easily than the external cell recycle system. (c) 1993 John Wiley & Sons, Inc.