Production of the siderophore enterobactin: use of four different fermentation systems and identification of the compound by HPLC

The article describes four different fermentation procedures for Escherichia coli AN311, a producer of enterobactin. A regular rotary shaker culture with a biphasic system consisting of an agar layer (as a reservoir for feeding processes) and a layer of liquid medium, 2.4 L and 10 L batch cultures, and a novel dialysis membrane fermentor were used. With the use of this latter fermentor type, the production of enterobactin could be increased by a factor of about 9.5, while growth increased by a factor of 12 compared to the other systems. For the rapid and reliable quantification of the concentration and purity of enterobactin an analytical and preparative high-performance liquid chromatography (HPLC) method was established. The degradation compounds of this siderophore were detected by diodearray and bioassays. A comparison of total catechol production as well as the distribution between enterobactin and its degradation compounds is given. (c) 1993 John Wiley & Sons, Inc.     

Continuous production of ethanol by yeast "immobilized" in a membrane-contained fermentor

A dialysate-feed, immobilized-cell dialysis continuous fermentation system was investigated as a method of relieving product inhibition in the conversion of glucose to ethanol by cells of Saccharomyces cerevisiae ATCC 4126. The substrate was fed into a continuous dialysate circuit and then into a batch fermentor circuit via diffusion through the microporous membranes of an intermediate dialyzer. Simultaneously, product was withdrawn from the fermentor circuit through the dialyzer membranes into the dialysate circuit and out in the effluent. Since the fermentor was operated without an effluent, the cells essentially were immobilized and converted substrate to product by maintenance metabolism. Contrary to prior results with this novel system for the continuous fermentation of lactose to lactate by lactobacillus cells, a steady state of yeast cells in the fermentor did not occur initially but was obtained by the depletion of medium nitrogen and the prevention of cell breakage, although the substrate and product concentrations then became unsteady. The inherent advantages of the system was offset in the ethanol fermentation by relatively low productivity, which appeared to be limited by membrane permeability.     

High cell density culture of a recombinant Escherichia coli producing penicillin acylase in a membrane cell recycle fermentor

A recombinant Escherichia coli HB101(pPAKS2) producing penicillin acylase was cultured in a membrane cell recycle fermentor. The strain was very stable throughout the whole experiment. The main inhibitory by-product was acetic acid, and cell growth ceased when its concentration was above 14 g/L Cell density could be increased up to 145 g/L dry weight without experiencing by-product inhibition by regulating glucose concentration in the fermentor and by using total membrane recycle. Acetic acid formation was negligible not only when cells were cultured in medium containing no glucose but also when glucose was limited. Dissolved oxygen control as well as glucose limitation was an indispensable condition for minimizing acetic acid formation when the medium contained glucose. Low concentrations of accumulated acetic acid were reused when glucose was limited. Use of highly concentrated medium reduced the membrane surface area required for cell recycle greatly. The recycle fermentor could be operated in various operational modes including partial bleed and repeated recycle culture to give high productivity. Productivity of a repeated recycle system was over 10 times higher than that of a simple batch system.     

Experimental simulation of oxygen profiles and their influence on baker's yeast production: II. Two-fermentor system

A reactor configuration consisting of two reactors with an exchange flow was used for the experimental simulation of large-scale conditions. The influence of fluctuations in oxygen concentration on the growth and metabolite production of baker's yeast was investigated by sparging one fermentor with air and one with nitrogen gas. It was found that the biomass yield decreased and the metabolite formation increased with rising circulation time (longer oxygen-unlimited and oxygen-limited periods). Not only was the performance of the oxygen-limited fermentor characterised by (partly) reductive metabolism, but that of the oxygen-unlimited fermentor as well. The results of the experiments in this reactor system were compared with those from the experiments carried out in a one-fermentor system with periodically changing oxygen concentrations. The formation of acetic acid, which is characteristic for transient states, showed a distinct difference between the two reactor systems.     

Dialysis Continuous Process for Ammonium-Lactate Fermentation: Improved Mathematical Model and Use of Deproteinized Whey

Separate terms for substrate limitation and product inhibition were incorporated into an equation describing the rate of cell growth for the steady-state fermentation of lactose to lactic acid with neutralization to a constant pH by ammonia. The equation was incorporated into a generalized mathematical model of a dialysis continuous process for the fermentation, developed previously, in which the substrate is fed into the fermentor and the fermentor contents are dialyzed through a membrane against water. The improved model was used to simulate the fermentation on a digital computer, and the results agreed with previous experimental tests using whole whey as the substrate. Further simulations were then made to guide experimental tests using deproteinized whey as the substrate. Dried cheese-whey ultrafiltrate was rehydrated with tap water to contain 242 mg of lactose per ml, supplemented with 8 mg of yeast extract per ml, charged into a 5-liter fermentor without sterilization, adjusted in pH (5.5) and temperature (44°C), and inoculated with an adapted culture of Lactobacillus bulgaricus. The fermentor and dialysate circuits were connected, and a series of steady-state conditions was managed nonaseptically for 71 days. The fermentation of deproteinized whey relative to whole whey, with both highly concentrated, resulted in similar extents of product accumulation but at a lesser rate.     

Biodegradation of dichloroacetic acid by freely suspended and adsorptive immobilized Xanthobacter autotrophicus GJ10 in soil

Xanthobacter autotrophicus GJ10 was applied in a packed-bed fermentor to degrade dichloroacetic acid (DCA) in batch-, semicontinuous and continuous culture. Degradation has been studied with freely suspended and adsorptive immobilized cells. To imitate natural soil systems, the fermentor was filled with sand. Concentrations of up to 20 mm DCA were degraded completely. If higher initial concentrations were used, the decrease in pH value inhibited further growth and degradation. In continuous culture the fermentor was inoculated additionally with activated sludge. Over a period of 2 weeks the specialized strain could be retained and no decrease in metabolic activity was observed. A decrease in degradation of DCA was observed when succinate was added as a second substrate. The haloacid dehalogenase was found to be induced by DCA. Non-induced cells showed typical repression of catabolites and diauxic growth with succinate as co-substrate. The results demonstrate that X. autotrophicus GJ10 might be suitable for applications in biological waste treatment systems. Correspondence to: H.-J. Rehm     

脱色希瓦氏菌(Shewanella decolorationis) S12还原不同电子受体的厌氧发酵罐培养方法

脱色希瓦氏菌Shewanella decolorationisS12在厌氧环境下能够使用多种电子受体进行厌氧呼吸。为了取得足够的细胞量用于膜蛋白质组学等科学研究的需要,本研究选取无机小分子(硝酸钠)、金属离子(柠檬酸铁)和有机大分子(偶氮染料苋菜红)作为电子受体,在使用确定成分的无机盐培养基条件下,使用不同浓度的电子供体和碳源对S12进行厌氧条件下静置和发酵罐的优化培养,采用连续补充电子受体的培养方式,确认了电子供体和碳源的合适浓度,建立了S12厌氧发酵罐培养方法。相比传统的静置厌氧培养,厌氧发酵罐培养方法在保证了严格厌氧条件下高效率还原电子受体的同时,还极大的提高了细胞生长密度。连续补充电子受体的厌氧发酵罐培养的S12最大细胞密度最大分别可达到静置厌氧培养细胞密度的325,304,369倍,而生长时间也比静置厌氧培养分别缩短了26.5%,17.6%,7.5%。这为需要大量细胞和蛋白的细菌厌氧呼吸生长实验建立了可行方法,对于进行兼性厌氧呼吸的微生物的大规模厌氧培养具有借鉴意义。     

Two-stage continuous process development for the production of medium-chain-length poly(3-hydroxyalkanoates)

Pseudomonas oleovorans forms medium-chain-length poly(3-hydroxyalkanoate) (PHA) most effectively at growth rates below the maximum specific growth rate. Under adequate conditions, PHA accumulates in inclusion bodies in cells up to levels higher than half of the cell mass, which is a time-consuming process. For PHA production, a two-stage continuous cultivation system with two fermentors connected in series is a potentially useful system. It offers production of cells at a specific growth rate in a first compartment at conditions that lead cells to generate PHA at higher rates in a second compartment, with a relatively long residence time. In such a system, dilution rates of 0.21 h(-1) in the first fermentor (D(1)) and 0.16 h(-1) in the second fermentor (D(2)) were found to yield the highest volumetric PHA productivity. Transient-state experiments allowed investigation of D(1) and D(2) over a wide dilution rate range at high resolution in time-saving experiments. Furthermore, the influence of temperature, pH, nutrient limitation, and carbon source on PHA productivity was investigated and results similar to optimum conditions in single-stage chemostat cultivations of P. oleovorans were found. With all culture parameters optimized, a volumetric PHA productivity of 1.06 g L(-1) h(-1) was determined. Under these conditions, P. oleovorans cells contained 63% (dry weight) PHA in the effluent of the second fermentor. This is the highest PHA productivity and PHA content reported thus far for P. oleovorans cultures grown on alkanes.     

Measurement of minimum substrate concentration (Smin) in a recycling fermentor and its prediction from the kinetic parameters of Pseudomonas strain B13 from batch and chemostat cultures.

The minimum substrate concentration required for growth, Smin, was measured for Pseudomonas sp. strain B13 with 3-chlorobenzoate (3CB) and acetate in a recycling fermentor. The substrates were provided alone or in a mixture. Smin values predicted with kinetic parameters from resting-cell batches and chemostat cultures differed clearly from the values measured in the recycling fermentor. When 3CB and acetate were fed as single substrates, the measured Smin values were higher than the individual Smin values in the mixture. The Smin in the mixture reflected the relative energy contributions of the two substrates in the fermentor feed. The energy-based maintenance coefficients during zero growth in the recycling fermentor were comparable for all influent compositions (mean +/- standard deviation, 0.34 +/- 0.07 J mg [dry weight]-1 h-1). Maintenance coefficient values for acetate were significantly higher in chemostat experiments than in recycling-fermentor experiments. 3CB maintenance coefficients were comparable in both experimental systems. The parameters for 3CB consumption kinetics varied remarkably with the experimental growth conditions in batch, chemostat, and recycling-fermentor environments. The results demonstrate that the determination of kinetic parameters in the laboratory for prediction of microbial activity in complex natural systems should be done under conditions which best mimic the system under consideration.     

Continuous culture in combined backmix-plug-flow-tubular-loop fermentor configurations

Several combinations of backmix, tubular-loop, and plug-flow fermentors with and without culture recycle were studied by computer simulations. The steady-state concentrations of cell mass in a continuous culture were calculated as a function of dilution rate using Monod growth kinetics. It was found theoretically and verified for one case experimentally that the maximum dilution rate, over which microbial cells were washed out from the fermentor, could be elevated well beyond the maximum specific growth rate if a particular fermentor combination was used. A combination of two backmix fermentors has been analyzed previously by Sinclair and Brown. Application of this type of fermentor combination as a seed tank for performing continuous culture of microbes in a plug-flow reactor was shown with special reference to fermentation production using the kinetics proposed by Luedeking and Piret, van Dedem and Moo-Young, and Brown and Vass.     

Electrochemical determination of cell populations

Summary Determination of cell populations was carried out using the potentiostatic systems. The system was constructed from two platinum electrodes and a saturated calomel electrode. The anode of a reference system was covered with cellulose dialysis membrane. The response time of the system was 3–5 min, and current differences between the two components were proportional to cell populations in a culture of Bacillus subtilis. Current differences were reproducible with an average relative error of 4%. Cell populations of B. subtilis in a fermentor could be continuously determined by using this new electrochemical method. Moreover, these systems can be sterilized by heat before use.     

The rotorfermentor. I. Description of the apparatus,power requirements,and mass transfer characteristics

A novel fermentation device, the rotorfermentor, is described and some experimental results are presented on power requirements and oxygen mass transfer characteristics of the rotorfermentor. This fermentation device is designed to achieve high cell concentrations in batch and continuous cultures. Basically, the rotorfermentor consists of a rotating microporous membrane which is enclosed within a stationary fermentor vessel. The metabolic products in the broth are continuously removed by filtration through the rotating microporous membrane while the growing cells can be retained inside the fermentor. This dual function of cell growth and concentration with the simultaneous removal of metabolic products is the essential characteristic of the rotorfermentor.     

Dialysis Continuous Process for Ammonium-Lactate Fermentation of Whey: Experimental Tests

Laboratory experiments were conducted to validate theoretical predictions describing a dialysis continuous process for the fermentation of whey lactose to ammonium lactate, in which the fermentor contents are poised at a constant pH by adding ammonia solution and dialyzed through a membrane against water. Dried sweet-cheese whey was rehydrated to contain 230 mg of lactose per ml, supplemented with 8 mg of yeast extract per ml, charged into a 5-liter fermentor without sterilization, adjusted in pH (5.3) and temperature (44°C), and inoculated with Lactobacillus bulgaricus. The fermentor and dialysate circuits were connected, and steady-state conditions were established. A series of such conditions was managed nonaseptically for 94 days to study the process and to demonstrate efficiency and productivity. As time progressed, the fermentation remained homofermentative and increased in conversion efficiency, although membrane fouling necessitated dialyzer cleaning about every 4 weeks. With a retention time of 19 h, 97% of the substrate was converted into products. Relative to nondialysis continuous or batch processes for the fermentation, the dialysis continuous process enabled the use of more concentrated substrate, was more efficient in the rate of substrate conversion, and additionally produced a second effluent of less concentrated but purer ammonium lactate.     

Design and physical characteristics of a multistage,continuous tower fermentor

A multistage tower laboratory fermentor has been constructed consisting of eight compartments separated by sieve plates. Flow of substrate and air is concurrent from the bottom to the top of the column. It, was hoped that this system could be used to reproduce, simultaneously on a continuous basis, eight distinct phases of a batch growth curve. It was believed that the extent of batch curve simulation would depend upon the character of hydraulic mean residence time of broth in the column and in the individual compartments. The expected relationship did not occur. Rather it was found that growth in the column involved residence time characteristics not only for the fluid but also for the microorganisms, and for the growth limiting substrate. Depending upon the column operation, these could be distinct and different. The purpose of this investigation was to study the residence time distribution (RTD) of the continous (fluid) and dispersed (microorganisms) phases for model systems as well as for a yeast fermentation. Various degrees of flow nonideality, i.e., fluid blackflow and dispersed phase sedimentation, were noticed. The former seems to be due to interaction of the concurrent gas and liquid flow; it is particularly dependent upon void area of the sieve plate holes. Sedimentation is probably a function of plate design as well as cell size and density. It wa concluded that for a particular plate design the gas hold-up wass controlled by superficial air velocity and was the main parameter governing the differences between dispersed and continous phase(Rt1). This conclusion was supported by a computeraided styudy utilizing a mathematical model of fluid flow to fit the growth kinetics and cell distribution observed experimentally throughout the fermentor. Some advantages of foam control in the tower fermentor by surface active compounds are mentioned. Also, suggestions are made for carrying out fermentations that have two liquid phases, such as a hydrocarbon fermentation. The possibility of closely approximating plug-flow conditions in the multistage tower fermentor, a necessary condition for batch growth simulation, is discussed from a practical point of view.     

Control of ammonium concentration in Escherichia coli fermentations

A control system has been devised for the maintenance of stable ammonium concentrations throughout a fedbatch fermentation. The control system is based on an ammonia gas-sensing electrode that monitors a pH-adjusted effluent stream from the fermentor. To overcome the time lag between the fermentor and the electrode, feedback control included metered flows of ammonium to both the fermentor and the electrode vessel. The system was used to study the growth of Escherichia coli B (ATCC 11303) at controlled ammonium concentrations of 5 to 200mM. Apparent specific growth rates, biomass and protein production, and glucose yields were essentially constant from 5 to 170mM. Above 170mM ammonium growth was inhibited. As ammonium concentration decreased from 170 to 5mM, ammonium yields increased from 1 to 24 g cell dry wt/g ammonium utilized. The results demonstrate that control of ammonium concentrations at levels so low that ammonium would be exhausted in batch fermentations can significantly increase overall ammonium yields.     

A dense cell retention culture system using stirred ceramic membrane reactor

A novel reactor design incorporating porous ceramic tubes into a stirred jar fermentor was developed. The stirred ceramic membrane reactor has two ceramic tubular membrane units inside the vessel and maintains high filtration flux by alternating use for filtering and recovering from clogging. Each filter unit was linked for both extraction of culture broth and gas sparging. High permeability was maintained for long periods by applying the periodical control between filtering and air sparging during the stirred retention culture of Saccharomyces cerevisiae. The ceramic filter aeration system increased the k(L)a to about five times that of ordinary gas sparing. Using the automatic feeding and filtering system, cell mass concentration reached 207 g/L in a short time, while it was 64 g/L in a fed-batch culture. More than 99% of the growing cells were retained in the fermentor by the filtering culture. Both yield and productivity of cells were also increased by controlling the feeding of fresh medium and filtering the supernatant of the dense cells culture. (c) 1994 John Wiley & Sons, Inc.     

A fiber-optic retroreflective turbidimeter for continuously monitoring cell concentration during fermentation

A fiber-optic retroreflective turbidimeter has been developed to automatically and continuously assay the cell concentration in a fermentor by measuring the turbidity of the solution as a function of the light scattered at 180° to the incident light. The output signal is nearly directly proportional to the cell concentration in a fermentor when the sample stream contains from 0 to more than 50 g of cells per liter (wet weight). The device consists of a bifurcated fiber-optics light pipe with its distal end inserted into a flow cell through which the material to be analyzed passes. A light source on one proximal branch of the light pipe illuminates the sample stream; light that is back-scattered from participates in the stream re-enters the light pipe and is returned to a photodetector on the other proximal branch of the light pipe. A signal conditioning system connected to the optical head by a cable provides gain and zero adjustment.     

Lipase production of Staphylococcus carnosus in a dialysis fermentor

Summary In a newly constructed one-vessel dialysis fermentor, a strain of Staphylococcus carnosus TM300 carrying the lipase secretion plasmid pLipPS1 was used to investigate exoenzyme and biomass production. The bacterial culture grows in an inner compartment of 21 volume, separated from a 101 nutrient broth compartment by a conventional dialysis membrane. In order to avoid substrate depletion and to prolong the growth phase, a highly concentrated nutrient broth was used. The biomass production reached 60 g cell dry weight/l. The increase in extracellular lipase concentration was directly coupled with the increase of cell mass and reached a value of 230 mg/l culture supernatant. Harvesting the cells in the late growth phase, the lipase content was about 30% of the total exoproteins in the supernatant.     

Analysis of two-stage recombinant bacterial fermentations using a structured kinetic model

A structured kinetic model has been employed to analyze the performance of a two-stage continuous fermentation of a recombinant Escherichia coli. Separating the cell growth phase from the gene expression phase in two fermentors minimizes the growth rate difference between the recombinant cells and the plasmid-free cells in the first fermentor, thereby increasing the plasmid stability. The plasmid-harboring cells from the first fermentor are continuously fed into the second fermentor, in which the foreign protein synthesis is turned on by the addition of the inducer. Consequently, the recombinant cells experience an immediate reduction in growth rates as soon as they enter the second stage and then recover to synthesize the foreign protein. To analyze the fermentation performance contributed by these cells with different intracellular foreign protein levels and growth rates, a novel method for determining the residence time distribution of the growing cells in the second stage has been formulated. Combined with this method, the structured kinetic model for recombinant bacterial cells is used to predict the plasmid stability and foreign productivity at various operation conditions, such as induction strength and dilution rates. This model can provide us with thorough understanding of the characteristics of the two-stage fermentations, and is useful for the development of large scale continuous cultures of recombinant bacteria.     

Control of autolysis of Bacillus subtilis for selective production of the intracellular enzyme glucose-6-phosphate dehydrogenase in aqueous two-phase systems

A method for the release of intracellular enzyme by autolysis of Bacillus subtilis cells is presented. Both the growth and lysis processes were further applied to aqueous two-phase systems (ATPS). Lysis induced by the addition of Triton X-100 and by low-temperature treatment facilitated the release of cytoplasmic enzyme glucose-6-phosphate dehydrogenase (G6PDH) in ATPS. The release selectivity increased when lysis was regulated by the addition of 50 μM or 100 μM Triton X-100. Cardiolipin efficiently inhibited the autolytic process. Control of the autolytic system promoted the selective release of G6PDH. B. subtilis cells could be grown and lysed in aqueous two-phase systems in a similar fashion to the conventional single-phase medium solutions. The released enzymes were partitioned according to their surface properties. G6PDH were extracted to the top phase in a PEG1540/Dex100K-200K sytem. Cells were partitioned to the bottom phase or the interface, and could be recycled into the fermentor. The selectivity of enzyme production was also increased in two-phase systems by the addition of cardiolipin.