Optimizing the continuous production of Candida utilis and Saccharomycopsis fibuliger on potato processing wastewater.

The yeasts Candida utilis and Saccharomycopsis fibuliger were propagated as a source of single-cell protein in a continuous, mixed, aerobic, single-stage cultivation on blancher water generated during potato processing. A series of steady-state experiments based on a two-level factorial design, half-replicate modified with an intermediate experiment, was performed to determine the effect of pH, 3.8 to 4.8; dissolved oxygen, 42 to 80% saturation; dilution rate, 0.17 to 0.31 h(-1); and temperature, 27 to 32 degrees C on the amount of carbon consumed, the rate of carbon consumption (R(c)), the amount of reducing sugar consumed, the rate of sugar consumption (R(g)), the amount of protein produced, the rate of protein production (R(p)), the yield from carbon, and the yield from reducing sugar. The results were analyzed by stepwise multiple regression and Fisher's least significant difference test. Analyses showed that high dilution rates resulted in increased R(c), R(g), and R(p) and indicated that a rate of 0.31 h(-1) was below the critical dilution rate. A temperature of 32 degrees C increased the amount of carbon consumed by 34%. A pH of 4.3 to 4.8 increased the amount of protein produced. The yield from carbon was constant, and the relatively high yield from reducing sugar indicated that other substrates were consumed. Dissolved oxygen was in excess at 42% saturation and above. Since C. utilis predominated the mixed cultures and amylase production appeared to be limited, a single-stage fermentation lacked efficiency. The experimental design allowed preliminary optimization of major environmental variables with relatively few experiments and provided a basis for future kinetic studies.     

Continuous cultivation of the yeast Candida utilis at different dilution rates on pineapple cannery effluent

Candida utilis was grown on a pineapple cannery effluent in a chemostat at dilution rates ranging between 0.05 and 0.65 h^–1 to establish optimal conditions for biomass production and chemical oxygen demand (COD) reduction. Sucrose, fructose and glucose were the main sugars in the effluent. Maximum value for cell yield coefficient and productivity were (0.686, g_x/g_s) and (2.96, g_x/l/h) at a dilution rate of 0.425 and 0.475 h^–1, respectively, while maximum COD reduction (98%) was attained at a dilution rate of 0.1 h^–1. The maintenance coefficient attained a value of (0.093, g_s/g_x/h). An increase in dilution rate produced a higher protein content of the biomass.     

Production of high-quality edible protein from Candida yeast grown in continuous culture

Candida utilis NRRL Y-900 was grown in aerobic continuous culture with cane molasses as the source of the growth-limiting carbon. At 1% reducing sugar in the chemostal (10 liter working volume) feed medium, addition of Zn (25μM) to a minimal salts medium resulted in an increase in the biomass productivity of the chemostat from 1.7 to 2.6 g/liter/hr with a growth yield of 0.55 g dry biomass/g reducing sugar utilized at D_max. On the average, the yeast biomass was 50–55% protein. At S_R > 2% sugar, the biomass productivity was limited by the oxygen supply. With O₂-supplemented aeration (at S_R = 4.2%)the maximum biomass productivity Was 7.25 g/liter/hr. Aerobic ethanol production was not observed. A highquality undenatured protein fraction was isolate from the yeast homogenate by isoelectric precipitation at pH 4.5. Contaminating nucleic acid was removed as an insoluble complex by chelation with an organic cation (cetavlon). The final protein product contained about 3% RNA (DWB) and was suitable for use as a food additive.     

Microbial production of propionic acid and vitamin B12 using molasses or sugar

With a cell concentration of 125 g dry biomass 1^–1 and a dilution rate of 0.1 h^–1,Propionibacterium acidipropionici produces 30 g propionic acid 1^–1 from sugar with a productivity of 3 g 1^–1 h^–1. The yield of propionic acid is approx. 0.36–0.45 g propionic acid g^–1 sucrose and is independent of the dilution rate and cell concentration. Acetic acid is an unwanted by-product in the production of propionic acid. The concentration of acetic acid only increases slightly when the cell concentration is increased. A two-stage fermentation process was developed for the conversion of sugar or molasses of various types to propionic acid and vitamin B₁₂. By fermentation of blackstrap molasses (from sugar beet and sugar cane) in the first fermentation stage 17.7 g propionic acid 1^–1 with a yield of 0.5 g propionic acid g^–1 carbohydrate was produced with a dilution rate of 0.25 h^–1. In the second stage 49 mg vitamin B₁₂ 1^–1 was produced at a dilution rate of 0.03 h^–1.     

Effect of dilution rate on growth characteristics of Candida utilis in multistage culture systems with different interstage mixing

The effect of dilution rate on important process parameters of biomass production in two multistage culture systems with different interstage mixing has been examined. Experiments were performed in a multistage tower fermenter and in a cascade of fermenters. Measurements were made at steady-state of continuous culture under constant and identical values of ethanol concentration of 50 gl^?1 in the feed, temperature, OTR and pH in both culture systems used. The microorganism used was Candida utilis. Ethanol inhibition influenced cell growth rate due to the complete dissimilation of the restricted quantity of acetate to H₂O and CO₂, leading to insufficient energy generation. The value of ethanol concentration at which ethanol started to inhibit cell growth was a combined function of OTR, S_R and D. The presence of the interstage mixing resulted in more efficient ethanol conversion to biomass in the whole range of dilution rates and significantly lowered the risk of washing-out at high values of both S_R and D.     

Studies on the variables and kinetics of SCP production from nopal fruit juice

Summary Submerged batch cultivation under controlled environmental conditions of pH 3.8, temperature 30°C, and K_La200 h^–1 (above 180 mMO₂ l ^–1 h^–1 oxygen supply rate) produced a maximum (12.0 g·l ^–1) SCP (Candida utilis) yield on the deseeded nopal fruit juice medium containing C/N ratio of 7.0 (initial sugar concentration 25 g·l ^–1) with a yield coefficient of 0.52 g cells/g sugar. In continuous cultivation, 19.9 g·l ^–1 cell mass could be obtained at a dilution rate (D) of 0.36 h^–1 under identical environmental conditions, showing a productivity of 7.2 g·l ^–1·h^–1. This corresponded to a gain of 9.0 in productivity in continuous culture over batch culture. Starting with steady state values of state variables, cell mass (C_X–19.9 g·l ^–1), limiting nutrient concentration (C_ln–2.5 g·l ^–1) and sugar concentration (C_S–1.5 g·l ^–1) at control variable conditions of pH 3.8, 30°C, and K_La 200 h^–1 keeping D=0.36 h^–1 as reference, transient response studies by step changes of these control variables also showed that this pH, temperature and K_La conditions are most suitable for SCP cultivation on nopal fruit juice. Kinetic equations obtained from experimental data were analysed and kinetic parameters determined graphically. Results of SCP production from nopal fruit juice are described.Nomenclature C_ln concentration of ammonium sulfate (g·l ^–1) - C_S concentration of total sugar (g·l ^–1) - C_X cell concentration (g·l ^–1) - D dilution rate (h^–1) - K_ln Monod's constant (g·l ^–1) - m maintenance coefficient (g ammonium sulfate cell^–1 h^–1) - m_(S) maintenance coefficient (g sugar g cell^–1 h^–1) - t time, h - Y yield coefficient (g cells/g ammonium sulfate) - Y_m maximum of Y - Y_S yield coefficient based on sugar consumed (g cells · g sugar^–1) - Y_S(m) maximum value of Y_S - ^µm maximum specific growth rate constant (h^–1)     

Growth and physiology of a yeast cultivated in batch and continuous culture systems

Inoculum size has been found to affect significantly the maximum attainable specific growth rate during batch cultivation ofCandida utilis. Lower inoculum size resulted in an increased growth rate and relatively longer lag. The culture is found to be most active in the beginning of the exponential phase as regards its RNA synthesis rate. Batch data were used for predicting the conditions of the yeast population in single-stage continuous culture system. Predicted and the experimental values showed a reasonable agreement. In single-stage chemostat the physiology of the yeast was studied on the basis RNA, DNA and protein synthesis rates at various growth rates. The results indicate that the productivity of cells and the rate of synthesis of macromolecules is highest at the dilution rate values of 0.33 to 0.35 hr⁻¹. In order to attain so-called unrestricted conditions of growth a pluristage pluristream continuous system was employed. It is assumed that under such conditions the specific growth rate and the synthetic activity of yeasts may reach its maximum on a given medium. The results presented do not show such conditions of growth under the experimental conditions employed (D ₁=0.35 hr⁻¹ andD ₂=0.2 to 1.7 hr⁻¹) withCandida utilis cultivated on beet molasses medium. Second stage of a two-stage two-stream continuous system is constantly fed with the cells from the foregoing stage; this category of cells on entering the new conditions of the second stage is expected to show some adaptation period. Experiments are reported to this effect.     

Optimization of dilution rate for the production of value added product and simultaneous reduction of organic load from pineapple cannery waste

Candida utiilis NRRL Y-900 was grown on pineapple cannery waste as the sole carbon and energy source in a chemostat at dilution rates ranging between 0.05 and 0.65 h⁻¹ to determine the growth kinetics. The cell yield coefficient varied with dilution rate and a maximum value of 0.662 ± 0.002 g_x/g_carb was obtained at a dilution rate of 0.4 h⁻¹. At steady state, the concentrations of carbohydrate, reducing sugar, and chemical oxygen demand (COD) appeared to follow Monod kinetics. At maximum specific growth rate (μ_max) 0.65 h⁻¹, the saturation constants for carbohydrate, reducing sugar and COD were 0.51 ± 0.02 g_carb/1, 0.046 ± 0.003 g_rs/1, and 1.036 ± 0.001 g_COD/1, respectively. Maximum biomass productivity (Q _{x max}) 2.8 ± 0.03 g_x/1 h was obtained at a dilution rate of 0.5 h⁻¹. At this dilution rate, only 71.0 ± 0.41% COD was removed whereas at a dilution rate of 0.1 h⁻¹, 98.2 ± 0.35% reduction in COD was achieved. At a dilution rate of 0.4 h⁻¹, the optimal yeast productivity and reduction in COD were 2.7 ± 0.13 g_p/1 h, and 84.2 ± 0.42%, respectively. This revised version was published online in July 2006 with corrections to the Cover Date.     

Effect of the dilution rate on the biomass yield ofBacillus thuringiensis and determination of its rate coefficients under steady-state conditions

Depending on the biomass yield on glucose and the cell morphology ofBacillus thuringiensis, three different metabolic states were observed in continuous culture. At dilution rates between 0.18 h^–1 and 0.31 h^–1 vegetative cells, sporulating bacteria and spores coexisted, while glucose and amino acids were consumed. Only vegetative cells were observed at dilution rates between 0.42 h^–1 and 0.47 h^–1 and glucose was used as the main carbon and energy source. AtD = 0.50 h^–1 the biomass yield on glucose decreases sharply. To define better the specific growth rate range in which the microorganism uses mainly glucose, a dilution rate of 0.25–0.45 h^–1 was studied. The experimental data could be adjusted to a Monod model and the following rate coefficients and growth yields were determined: maximum specific growth rate 0.54 h^–1, saturation constant 0.56 mg glucose ml^–1, biomass growth yields 0.43 g cells (g glucose)^–1, and 0.76 g cells (g oxygen)^–1, and maintenance coefficients 0.065 g glucose (g cells)^–1 h^–1 and 0.039 g oxygen (g cells)^–1 h^–1.     

Glycerol production by Candida krusei employing NaCl as an osmoregulator in batch and continuous fermentations

Addition of 40 g NaCl l^–1 to a chemically defined medium containing 140 g glucose l^–1 in shake-flask culture improved glycerol production by Candida krusei from 16.5 g l^–1 to 47.7 g l^–1. With 40 g NaCl l^–1 at a dilution rate of 0.065 h^–1, glycerol concentration, glycerol yield (based on glucose consumed), and productivity in a four-stage cascade bioreactor were higher by 240%, 27% and 28%, respectively, than in a single-stage continuous culture system.     

Influence of acetate on the growth of Candida utilis in continuous culture

Candida utilis was grown on acetate in chemostat cultures that were, successively, carbon and ammonia-limited (30° C; pH 5.5). With carbon(acetate)-limited cultures, the specific rate of oxygen consumption (q _{O 2}) was not a linear function of the growth rate but was markedly stimulated at the higher dilution rates, thus effecting a marked decrease in the Y _O value. This increased respiration rate, and decreased yield value, correlated closely with a marked increase in the extracellular acetate concentration. Under ammonia-limiting conditions, very low Y _O values were found, generally comparable with those found with carbon-limited cultures growing at the higher dilution rates, but these varied markedly with the extracellular acetate concentration. Thus, when the unused acetate concentration was raised progressively from about 5 g/l to about 21 g/l, the Y _O value decreased non-linearly from 11.4 to 5.8. When the extracellular acetate concentration was further increased to 25 g/l, growth was inhibited and the culture washed out. This relationship between respiration rate and the extracellular concentration of unused acetate was also markedly influenced by the culture pH value. Thus, with a fixed extracellular acetate concentration (16±2g/l) and dilution rate (0.14 h^–1), lowering the culture pH value progressively from 6.9 to 5.1 effected a marked and progressive increase in the respiration rate. Further lowering of the culture pH to 4.8, however, caused a complete collapse of respiration. In contrast to this situation, progressively lowering the pH value of an acetatelimited culture from 6.9 to 4.5 affected only slightly the culture respiration rate, and growth was possible even at a pH value of 2.5. These results are discussed in the context of the possible mechanisms whereby acetate exerts its toxic effect on the growth of C. utilis.     

Continuous Production of Long-Side-Chain Poly-β-Hydroxyalkanoates by Pseudomonas oleovorans

Shake flask experiments showed that Pseudomonas oleovorans began to be growth inhibited at 4.65 g of sodium octanoate liter^-1, with total inhibition at 6 g liter^-1. In chemostat studies with 2 g of ammonium sulfate and 8 g of octanoate liter^-1 in the feed, the maximum specific growth rate was 0.51 h^-1, and the maximum specific rate of poly-β-hydroxyalkanoate (PHA) production was 0.074 g of PHA g of cellular protein^-1 h^-1 at a dilution rate (D) of 0.25 h^-1. When the specific growth rate (μ) was <0.3 h^-1, the PHA composition was relatively constant with a C₄/C₆/C₈/C₁₀ ratio of 0.1:1.7:20.7:1.0. At μ > 0.3 h^-1, a decrease in the percentage of C₈ with a concomitant increase in C₁₀ monomers as μ increased was probably due to the effects of higher concentrations of unmetabolized octanoate in the fermentor. At D = 0.24 h^-1 and an increasing carbon/nitrogen ratio, the percentage of PHA in the biomass was constant at 13% (wt/wt), indicating that nitrogen limitation did not affect PHA accumulation. Under carbon-limited conditions, the yield of biomass from substrate was 0.76 g of biomass g of octanoate^-1 consumed, the yield of PHA was 0.085 g of PHA g of octanoate^-1 used, and 7.9 g of octanoate was consumed for each gram of NH₄⁺ supplied. The maintenance coefficient was 0.046 g of octanoate g of biomass^-1 h^-1. Replacement of sodium octanoate with octanoic acid appeared to result in transport-limited growth due to the water insolubility of the acid.     

Single cell protein production from mandarin orange peel

Summary As the hydrolysis of mandarin orange peel with macerating enzyme (40°C, 24 h) produced 0.59 g g^–1 reducing sugar per dry peel compared to 0.36 by acid-hydrolysis (15 min at 120°C with 0.8 N H₂SO₄), the production of single cell protein (SCP) from orange peel was studied mostly using enzymatically hydrolyzed orange peel.When the enzymatically hydrolyzed peel media were used, the utilization efficiency of reducing sugars (%) and the growth yield from reducing sugars (g g^–1) were: 63 and 0.51 for Saccharomyces cerevisiae; 56 and 0.48 for Candida utilis; 74 and 0.69 for Debaryomyces hansenii and 64 and 0.70 for Rhodotorula glutinis. SCP production from orange peel by D. hansenii and R. glutinis were further studied. Batch cultures for 24 h at 30°C using 100 g dried orange peel produced 45 g of dried cultivated peel (protein content, 33%) with D. hansenii and 34 g (protein content, 50%) with R. glutinis, and 38 g (protein content, 44%) with a mixture of both yeasts.     

Factors which influence the sedimentation characteristics of Torulopsis glabrata after growth in a recirculation system

Summary Some environmental affects on cell aggregation described in the literature are briefly summarized. By means of a biomass recirculation culture (Contact system), using the yeast Torulopsis glabrata, the aggregation behavior of cells in static and in dynamic test systems is described. Sedimentation times required to obtain 50 g · l^–1 yeast dry matter in static systems were always higher than in dynamic ones.In addition to, influencing the biomass yield, the specific growth rate of the yeast also affected cell aggregation. The specific growth rate and therefore the aggregation could be regulated by the biomass recirculation rate as well as by the sedimenter volume.Abbreviations f_o Overflow flow rate (l·h^–1) - f_R Recycle flow rate (l·h^–1) - f_t0t Total flow rate through the fermenter (l·h^–1) - g Gram - h Hour - D_R Fermenter dilution rate due to recycle (h^–1) - D_S Fermeter dilution rate due to substrate (h^–1) - D_tot Total fermenter dilution rate (h^–1) - l Liter - Specific growth rate (h^–1) - P_F Fermenter productivity (g·l^–1·h^–1) - P_FS Overall productivity (g·l^–1·h^–1) - R_pM Rates per minute - RS Residual sugar content in the effluent with respect to the substrate concentration (%) - Y Yield of biomass with respect to sugar concentration (%) - Sed 50 Sedimentation time to reach a YDM of 50 g·l^–1 (min) - V Volume (l) - V_F Fermenter volume (l) - V_Sed Sedimenter volume (l) - VVM Volumes per volume and minute - X_F YDM in the fermenter (g·l^–1) - X_F YDM in the recycle (g·l^–1) - X_S Yeast dry matter due to substrate concentration (g·l^–1) - YDM Yeast dry matter (g·l^–1)     

Energetics and product formation by Saccharomyces cerevisiae grown in anaerobic chemostats under nitrogen limitation

Anaerobic fermentation of glucose (20 g/l) by Saccharomyces cerevisiae CBS 8066 was studied in a chemostat (dilution rate = 0.05–0.25 h^–1) at different concentrations of the nitrogen source (5.00 g/l or 0.36 g/l ammonium sulphate). The ethanol yield (g ethanol produced/g glucose consumed) was found to be higher and the glycerol yield (g glycerol formed/g glucose consumed) lower during nitrogen limitation than under carbon limitation. The biomass yield on ATP (g dry weight biomass produced/mol ATP consumed) was consequently found to be lower during nitrogen-limited conditions.     

Effects of dilution rate and pH on the ruminal cellulolytic bacterium Fibrobacter succinogenes S85 in cellulose-fed continuous culture

The ruminal cellulolytic bacterium Fibrobacter succinogenes S85 was grown in cellulose-fed continuous culture at 22 different combinations of dilution rate (D, 0.014–0.076 h^-1) and extracellular pH (6.11–6.84). Effects of pH and D on the fermentation were determined by subjecting data on cellulose consumption, cell yield, product yield (succinate, acetate, formate), and soluble sugar concentrationto response surface analysis. The extent of cellulose conversion decreased with increasing D. First-order rate constants at rapid growth rates were estimated as 0.07–0.11 h^-1, and decreased with decreasing pH. Apparent decreases in the rate constant with increasing D was not due to inadequate mixing or preferential utilization of the more amorphous regions of the cellulose. Significant quantities of soluble sugars (0.04–0.18 g/l, primarily glucose) were detected in all cultures, suggesting that glucose uptake was rather inefficient. Cell yields (0.11–0.24 g cells/g cellulose consumed) increased with increasing D. Pirt plots of the predicted yield data were used to determined that maintenance coefficient (0.04–0.06 g cellulose/g cells · h) and true growth yield (0.23–0.25 g cells/g cellulose consumed) varied slightly with pH. Yields of succinate, the major fermentation endproduct, were as high as 1.15 mol/mol anhydroglucose fermented, and were slightly affected by dilution rate but were not affected by pH. Comparison of the fermentation data with that of other ruminal cellulolytic bacteria indicates that F. succinogenes S85 is capable of rapid hydrolysis of crystalline cellulose and efficient growth, despite a lower _max on microcrystalline cellulose.     

Continuous and biomass recycle fermentations of Clostridium acetobutylicum

Using experimental data from continuous cultures of Clostridium acetobutylicum with and without biomass recycle, relationships between product formation, growth and energetic parameters were explored, developed and tested. For glucose-limited cultures the maintenance models for, the Y _ATP and biomass yield on glucose, and were found valid, as well as the following relationships between the butanol (Y _B/G) or butyrate (Y _BE/G) yields and the ATP ratio (R _ATP, an energetic parameter), Y _B/G =0.82-1.35 R _ATP, Y _BE/G =0.54 + 1.90 R _ATP. For non-glucose-limited cultures the following correlations were developed, Y _B/G =0.57-1.07 , Y _B/G =0.82-1.35 R _ATPATP and similar equations for the ethanol yield. All these expressions are valid with and without biomass recycle, and independently of glucose feed or residual concentrations, biomass and product concentrations. The practical significance of these expressions is also discussed.List of Symbols D h^–1 dilution rate - m _e mol g^–1 h^–1 maintenance energy coefficient - m _G mol g^–1 h^–1 maintenance energy coefficient - R biomass recycle ratio, (dimensionless) - R _ATP ATP ratio (eqs.(5), (10) and (11)), (dimensionless) - X kg/m³ biomass concentration - Y _ATP g biomass per mol ATP biomass yield on ATP - Y _ATP ^max g biomass per mol ATP maximum Y _ATP - Y _A/G mol acetate produced per mol glucose consumed molar yield of acetate - y _an/g mol acetone produced per mol glucose consumed molar yield of acetone - Y _B/G mol butanol produced per mol glucose consumed molar yield of butanol - y _be/g mol butyrate produced per mol glucose consumed molar yield of butyrate - Y _E/G mol ethanol produced per mol glucose consumed molar yield of ethanol - Y _X/G g biomass per mol glucose consumed biomass yield on glucose - Y _ATP ^max g biomass per mol maximum Y _X/G glucose consumed - h^–1 specific growth rate     

Intermediary Metabolite Concentrations in Xylulose- and Glucose-Fermenting Saccharomyces cerevisiae Cells

Glucose and xylulose fermentation and product formation by Saccharomyces cerevisiae were compared in batch culture under anaerobic conditions. In both cases the main product was ethanol, with glycerol, xylitol, and arabitol produced as by-products. During glucose and xylulose fermentation, 0.74 and 0.37 g of cell mass liter⁻¹, respectively, were formed. In glucose-fermenting cells, the carbon balance could be closed, whereas in xylulose-fermenting cells, about 25% of the consumed sugar carbon could not be accounted for. The rate of sugar consumption was 3.94 mmol g of initial biomass⁻¹ h⁻¹ for glucose and 0.39 mmol g of initial biomass⁻¹ h⁻¹ for xylulose. Concentrations of the intermediary metabolites fructose-1,6-diphosphate (FDP), pyruvate (PYR), sedoheptulose 7-phosphate (S7P), erytrose 4-phosphate, citrate (CIT), fumarate, and malate were compared for both types of cells. Levels of FDP, PYR, and CIT were lower, and levels of S7P were higher in xylulose-fermenting cells. After normalization to the carbon consumption rate, the levels of FDP were approximately the same, whereas there was a significant accumulation of S7P, PYR, CIT, and malate, especially of S7P, in xylulose-fermenting cells compared with in glucose-fermenting cells. In the presence of 15 μM iodoacetate, an inhibitor of the enzyme glyceraldehyde-3-phosphate dehydrogenase (EC 1.2.1.12), FDP levels increased and S7P levels decreased in xylulose-assimilating cells compared with in the absence of the inhibitor, whereas fermentation was slightly slowed down. The specific activity of transaldolase (EC 2.2.1.2), the pentose phosphate pathway enzyme reacting with S7P and glyceraldehyde-3-phosphate, was essentially the same for both glucose- and xylulose-fermenting cells. It was, however, several orders of magnitude lower than that reported for a Torula yeast and Candida utilis. The presence of iodoacetate did not influence the activity of transaldolase in xylulose-fermenting cells. The results are discussed in terms of a competition between the pentose phosphate pathway and glycolysis for the common metabolite, glyceraldehyde-3-phosphate, which would explain the low rates of xylulose assimilation and ethanol production from xylulose by S. cerevisiae.     

A mixed yeast-bacteria process for the aerobic conversion of poultry waste into single-cell protein

Summary A mixed yeast-bacteria process was developed to convert poultry waste into a high protein feedstuff. A uricase producing strain ofCandida utilis was utilized with the, natural flora of the poultry manure. Molasses was used as carbon source. Variation of C/N consumed ratio with dilution rate was investigated and the product quality was compared with the other feedstuffs.     

Influence of Carbon Source on Nitrate Removal by Nitrate-Tolerant Klebsiella oxytoca CECT 4460 in Batch and Chemostat Cultures

The nitrate-tolerant organism Klebsiella oxytoca CECT 4460 tolerates nitrate at concentrations up to 1 M and is used to treat wastewater with high nitrate loads in industrial wastewater treatment plants. We studied the influence of the C source (glycerol or sucrose or both) on the growth rate and the efficiency of nitrate removal under laboratory conditions. With sucrose as the sole C source the maximum specific growth rate was 0.3 h⁻¹, whereas with glycerol it was 0.45 h⁻¹. In batch cultures K. oxytoca cells grown on sucrose or glycerol were able to immediately use sucrose as a sole C source, suggesting that sucrose uptake and metabolism were constitutive. In contrast, glycerol uptake occurred preferentially in glycerol-grown cells. Independent of the preculture conditions, when sucrose and glycerol were added simultaneously to batch cultures, the sucrose was used first, and once the supply of sucrose was exhausted, the glycerol was consumed. Utilization of nitrate as an N source occurred without nitrite or ammonium accumulation when glycerol was used, but nitrite accumulated when sucrose was used. In chemostat cultures K. oxytoca CECT 4460 efficiently removed nitrate without accumulation of nitrate or ammonium when sucrose, glycerol, or mixtures of these two C sources were used. The growth yields and the efficiencies of C and N utilization were determined at different growth rates in chemostat cultures. Regardless of the C source, yield carbon (Y_C) ranged between 1.3 and 1.0 g (dry weight) per g of sucrose C or glycerol C consumed. Regardless of the specific growth rate and the C source, yield nitrogen (Y_N) ranged from 17.2 to 12.5 g (dry weight) per g of nitrate N consumed. In contrast to batch cultures, in continuous cultures glycerol and sucrose were utilized simultaneously, although the specific rate of sucrose consumption was higher than the specific rate of glycerol consumption. In continuous cultures double-nutrient-limited growth appeared with respect to the C/N ratio of the feed medium and the dilution rate, so that for a C/N ratio between 10 and 30 and a growth rate of 0.1 h⁻¹ the process led to simultaneous and efficient removal of the C and N sources used. At a growth rate of 0.2 h⁻¹ the zone of double limitation was between 8 and 11. This suggests that the regimen of double limitation is influenced by the C/N ratio and the growth rate. The results of these experiments were validated by pulse assays.