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     

Accumulation of lipid byRhodotorula glutinis in continuous culture

Summary Rhodotorula glutinis accumulated 35% (w/w) lipid when grown nitrogen-limited in a chemostat at a dilution rate (D) of 0.02^–1 . At D = 0.10 h^–1, the lipid content was only 15% (w/w). Dual limitation of nitrogen and phosphate increased neither the amount of lipid produced nor the lipid yield (14g lipid per 100g glucose consumed). The fatty acid composition was unchanged by the growth rate.     

Development of a structured model for biopolymer synthesis in the fungus Aureobasidium pullulans

Previous modelling of the pullulan fermentation is discussed and found to lack any mechanistic basis. It is concluded that predictive ability can only be conferred by a structured model with at least two compartments, based upon the best available knowledge of the physiology of the microorganism. Such a model is constructed and compared with experimental data.List of Symbols A (gdm^–3)(g/l) Ammonium ion concentration - B (gdm^–3)(g/l) Concentration of balanced growth compartment of biomass - G (gdm^–3)(g/l) Glucose concentration - k _A (gdm^–3)(g/l) Saturation constant for ammonium - k _G (gdm^–3)(g/l) Saturation constant for glucose - k _S (gdm^–3)(g/l) Saturation constant for sucrose - P (gdm^–3)(g/l) Pullulan concentration - Q Quality of biomass=U/(U+B) - r _G (gdm^–1h^–1)(g/l/h) Rate of removal of glucose from broth - r _GB (gdm^–3h^–1)(g/l/h) Rate of incorporation of glucose into balanced compartment - r _GB (gdm^–3h^–1)(g/l/h) Rate of utilisation of glucose for energy production and cell maintenance - r _GP (gdm^–3h^–1)(g/l/h) Rate of conversion of glucose to pullulan - r _GU (gdm^–3h^–1)(g/l/h) Rate of incorporation of glucose into unbalanced compartment - r _s (gdm^–3h^–1)(g/l/h) Rate of conversion of sucrose to glucose - S (gdm^–3)(g/l) Concentration of sucrose - U (gdm^–3)(g/l) Concentration of unbalanced growth compartment of biomass - X (gdm^–3)(g/l) Biomass concentration - Y _G/A Grams of glucose consumed per gram of ammonium consumed - Y _G/B Grams of glucose consumed per gram of balanced biomass produced - Y _G/U Grams of glucose consumed per gram of unbalanced biomass produced - Y _G/P Grams of glucose consumed per gram of pullulan produced - Rate constant for conversion of sucrose to glucose - Rate constant for uptake of glucose by the cells - Model parameter governing inhibition of sucrose conversion and glucose utilisation - Model parameter denoting fraction of glucose uptake devoted to cell maintenance and energy production - Model parameter governing apportionment of glucose between pseudo-growth and pullulan production This work was funded by the National Engineering Laboratory (NEL) through the Bioreactor Design Club. The authors would like to express their gratitude to the NEL for this generous support.     

Ethanol fermentation by flocculating yeast: Performance and stability dependence on a critical fermentation rate

Summary A system coupling fermentor and decantor permitted strong accumulation of yeast flocs that were homogeneously suspended in the reactional volume. At 100–190 g/l glucose feed practically total substrate conversion was attained. At 130 g/l glucose feed the highest productivity (18.4 g.l.h) and the highest ethanol yield (90.6%) were reached with biomass levels of 80–90 g/l. We observed that the stability of this system is limited when a critical fermentation rate (D.S_o) close to 39–40 g/l.h (with corresponding ethanol productivities of 19–20 g/l.h) is reached. Higher fermentation rates provoked de-flocculation and lost of biomass.Symbols D dilution rate (h^–1) - E ethanol (g/l) - S_r residual substrate (g/l) - S_o substrate in the feed (g/l) - X biomass (g/l) - ethanol yield (%) - DS_o fermentation rate (g/l.h) (for S_r0) - P_E ethanol productivity (g/l.h)     

By-product formation by a novel glycerol-producing yeast,Candida glycerinogenes,with different O2 supplies

Candida glycerinogenes is an aerobe which does not depend on sulphite for production of glycerol. With a sufficient O₂ supply, up to 130 g glycerol l^–1 was produced with 2.6 g acetic acid l^–1 as by-product. However, with an insufficient O₂ supply – with higher volumes of medium or at higher corn steep liquid concentrations – the glycerol concentration was lower because the by-products, ethanol, pyruvate and lactic acid, were produced in greater amounts, up to 45 g l^–1, 4.3 g l^–1, 1.6 g l^–1, respectively, whereas, less acetic acid (0.6 g l^–1) was produced. In addition, ethanol decreased to 0.4 g l^–1 and the glycerol yield improved from 34 to 50% (w/w) by adding 50 g sulphite l^–1, nevertheless, acetic acid increased to 7.8 g l^–1.     

Continuous and biomass recycle fermentations of Clostridium acetobutylicum

The availability and demand of biosynthetic energy (ATP) is an important factor in the regulation of solvent production in steady state continuous cultures of Clostridium acetobutylicum. The effect of biomass recycle at a variety of dilution rates and recycle ratios under both glucose and non-glucose limited conditions on product yields and selectivities has been investigated. Under conditions of non-glucose limitation, when the ATP supply is not growth-limiting, a lower growth rate imposed by biomass recycle leads to a reduced demand for ATP and substantially higher acetone and butanol yields. When the culture is glucose limited, however, biomass recycle results in lower solvent yields and higher acid yields.List of Symbols A ₆₀₀ absorbance at 600 nm - ATP adenosine triphosphate - C _imol/dm³ concentration of componenti in the fermentor - C _i ⁰ mol/dm³ concentration of componenti in the feed - D h^–1 dilution rate - F dm³/h feed flow rate - FdH₂ ferredoxin, reduced form - NAD nicotinamide adenine dinucleotide, oxidized form - NADH nicotinamide adenine dinucleotide, reduced form - NfF mmol/g/h NADH produced from oxidation of FdH₂ per unit biomass per unit time - P dm³/h filtrate flow during biomass recycle operation - PCRP C-mole carbon per C-mole glucose utilized percent of (substrate) carbon recovered in products - R recycle ratio,P/F - SPR mmol/g/h specific production rate - X _imol product/100 mol glucose utilized product yield - Y _ATP g biomass/mol ATP biomass yield on ATP - Y _GLU g biomass/mol glucose biomass yield on glucose - Y _ig biomass/mol biomass yield on nutrienti - h^–1 specific growth rate     

High productivity continuous ethanol fermentation with a flocculating mutant strain of Zymomonas mobilis

High fermenter (volumetric) ethanol productivities (80 g/lh^–1) were attained in a simple single-stage continuous-stirred-tank-reactor (CSTR) employing a flocculent mutant of Zymomonas mobilis with a feed containing 100g/l glucose. Under these conditions a final ethanol concentration of 47.6 g/l was obtained, representing a maximum conversion efficiency of 97% of theoretical.Nomenclature SR = Medium glucose concentration (g/l)X Biomass concentration (g/l) - P Ethanol concentration (g/l) - VP Volumetric productivity (g ethanol/l/h) - Yp/s Product yield coefficient (g ethanol/g glucose consumed) - Qp Specific rate of ethanol formation (g ethanol/g cells/h) - D Dilution rate (h^–1) - Dmax Maximum dilution rate: ie., highest dilution rate at which the effluent glucose concentration 4g/l (h^–1)     

Organic nitrogen of tomato waste hydrolysate enhances glucose uptake and lipid accumulation in Cunninghamella echinulata

Aims: To investigate the effect of organic nitrogen on lipogenesis during growth of Cunninghamella echinulata on tomato waste hydrolysate (TWH) media. Methods and Results: Cunninghamella echinulata grown on a TWH medium rapidly took up glucose and produced large amounts of lipids. However, when some quantities of the organic nitrogen were removed from TWH (by acid followed by alkaline precipitation of proteins) the uptake of glucose was dramatically reduced and large quantities of fungal biomass having low lipid content were produced. Nevertheless, when glycerol was used as carbon source instead of glucose, the uptake rate as well as the biomass production and the lipid accumulation processes were unaffected by the TWH organic nitrogen removal. Finally, when the fungus was grown on a glucose supplemented TWH medium that contained no assimilable organic nitrogen (after further precipitation of proteins with methanol), the produced biomass contained non-negligible quantities of lipids, although glucose uptake remained low. Lipid analysis showed that the produced lipids comprised mainly of neutral lipids, which were preferentially consumed during lipid turnover. Lipid production on the original TWH medium having glucose as carbon source was 0·48 g of lipid per gram of dry biomass, corresponding to 8·7 g of lipid per litre of growth medium. The produced lipids contained 11·7%γ-linolenic acid (GLA), hence the GLA yield was more than 1 g l⁻¹. Conclusions: Organic nitrogen compounds found in TWH favour glucose (but not glycerol) uptake and lipid accumulation in C. echinulata. Significance and Impact of the Study: Agro-industrial wastes containing organic nitrogen, such as tomato waste, are produced in vast amounts causing severe environmental problems. These wastes could be used as fermentation feedstock to produce microbial lipids.     

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.     

Estimation of the energetic biomass yield and efficiency of oxidative phosphorylation in cell-recycle cultures of Schizosaccharomyces pombe

The energetics of growth of the fission yeast Schizosaccharomyces pombe was studied in continuous high-cell concentration cultures using a cell-recycle fermentor. Under non-O₂-limited conditions, steady-states were obtained at various specific growth rates (partial cell-recycle) with purely oxidative (glucose limitation) or respiro-fermentative (glucose excess) metabolic behaviour. The stoichiometry of biomass synthesis was established from the elemental composition of the cells and measurements of all the specific metabolic rates, i.e. consumption of glucose and O₂ and production of CO₂, ethanol and other products. The theoretical yield factor for biomass on glucose was Y_G,X = 0.85 C-mol·C-mol^–1 and maintenance requirements were negligible. Assuming a constant coupling between energy generation and biomass formation for both respirative and respiro-fermentative breakdown of glucose, the biomass yield from ATP (Y_ATP) and the efficiency of oxidative phosphorylation (P/O ratio) could be determined as 9.8 g biomass·mol ATP and 1.28 mol ATP·atom of O₂, respectively. Correspondence to: A. Pareilleux     

Ethanol production by anaerobic thermophilic bacteria: Kinetics in fed-batch cultures ofClostridium thermohydrosulfuricum

Summary Fed-batch fermentations ofClostridium thermohydrosulfuricum are carried out using medium rich in nitrogen source and with glucose as growth limiting factor. The ethanol/lactate yield increases as the specific growth rate and specific rate of consumption of glucose diminish. Under the experimental conditions chosen here this yield attained 3.66 moles. mole^–1 with a maximal ethanol concentration of 12 g.l^–1. In batch fermentation, the maximum concentration of ethanol did not exceed 8 g.l^–1, independent of the concentration in glucose or nitrogen source applied.     

Microbial fed-batch production of 1,3-propanediol by Klebsiella pneumoniae under micro-aerobic conditions

The microbial production of 1,3-propanediol (1,3-PD) by Klebsiella pneumoniae under micro-aerobic conditions was investigated in this study. The experimental results of batch fermentation showed that the final concentration and yield of 1,3-PD on glycerol under micro-aerobic conditions approached values achieved under anaerobic conditions. However, less ethanol was produced under microaerobic than anaerobic conditions at the end of fermentation. The batch micro-aerobic fermentation time was markedly shorter than that of anaerobic fermentation. This led to an increment of productivity of 1,3-PD. For instance, the concentration, molar yield, and productivity of 1,3-PD of batch micro-aerobic fermentation by K. pneumoniae DSM 2026 were 17.65 g/l, 56.13%, and 2.94 g l^–1 h^–1, respectively, with a fermentation time of 6 h and an initial glycerol concentration of 40 g/l. Compared with DSM 2026, the microbial growth of K. pneumoniae AS 1.1736 was slow and the concentration of 1,3-PD was low under the same conditions. Furthermore, the microbial growth in fed-batch fermentation by K. pneumoniae DSM 2026 was faster under micro-aerobic than anaerobic conditions. The concentration, molar yield, and productivity of 1,3-PD in fed-batch fermentation under micro-aerobic conditions were 59.50 g/l, 51.75%, and 1.57 g l^–1 h^–1, respectively. The volumetric productivity of 1,3-PD under microaerobic conditions was almost twice that of anaerobic fed-batch fermentation, at 1.57 and 0.80 g l^–1 h^–1, respectively.     

The effect of pH on kinetic and yield parameters during the ethanolic fermentation of D-xylose with Pachysolen tannophilus

We have studied the ethanolic fermentation of D-xylose with Pachysolen tannophilus in batch cultures. We propose a model to predict variations in D-xylose consumed, and biomass and ethanol produced, in which we include parameters for the specific growth rate, for the consumption of D-xylose and production of ethanol either related or not to growth.The ideal initial pH for ethanol production turned out to be 4.5. At this pH value the net specific growth rate was 0.26 h^–1, biomass yield was 0.16 g.g^–1, the cell-maintenance coefficient was 0.073 g.g^–1.h^–1, the parameter for ethanol production non-related to growth was 0.064 g.g^–1,h^–1 and the maximum ethanol yield was 0.32 g.g^–1.List of Symbols A _c Carbon atomic weight - a _d1/h Specific cell-maintenance rate defined in Eq. (8) - c Mass fraction of carbon in the biomass - E g/l Ethanol concentration - f _x Correction factor defined in Eq. (13) - f _x Correction factor defined in Eq. (13) - f _xi Correction factor defined in Eq. (14) - k _d1/h Death constant - M _E Ethanol molecular weight - M _s Xylose molecular weight - M _xi Xylitol molecular weight - m g xylose/g biomass Maintenance coefficient for substrate - m _dg xylose/g biomass Maintenance coefficient when k _d - q _Eg ethanol/g biomass. Specific ethanol production rate - s g/l Residual xylose concentration - s ₀ g/l Initial xylose concentration - t h Time - x g/l Biomass concentration - x ₀ g/l Initial biomass concentration - Y _E/sg ethanol/g xylose Instantaneous ethanol yield - ¯Y _E/sg ethanol/g xylose Mean ethanol yield - Y _E ^s/T g ethanol/g xylose Theoretical ethanol yield - Y _E ^s/* g ethanol/g xylose Corrected instantaneous ethanol yield - ¯Y _E ^s/* g ethanol/g xylose Corrected mean ethanol yield - Y _x/sg biomass/g xylose Biomass yield - ¯Y _xi/sg xylitol/g xylose Mean xylitol yield Greek Letters g ethanol/g biomass Growth-associated product formation parameter - g ethanol/g biomass.h Non-growth-associated product formation parameter - _dg ethanol/g biomass.h Non-growth-associated product formation parameter when k _d0 - h Variable defined in Eq. (6) or Eq. (7) - 1/h Specific growth rate - _m1/h Maximum specific growth rate     

H2 production from chemostat fermentation of glucose byClostridium butyricum andClostridium pasteurianum in ammonium- and phosphate limitation

Summary In ammonium-limitation (4.55 mM NH₄ ⁺) at a dilution rate (D)=0.081 h^–1,Clostridium butyricum produced 2 mol H₂ per mol glucose consumed at pH 5.0, but at a low fermentation rate. At higher pH, important amounts of extracellular protein were produced. Phosphatelimitation (0.5 mM PO₄ ^–3) at D=0.061 h^–1 and pH 7.0 were the best conditions tested for hydrogen gas production (2.22 mol H₂ per mol glucose consumed) at a high fermentation rate. Steady-state growth at lower pH and with 0.1 mM PO₄ ^–3 resulted in proportional higher glucose incorporation into biomass and lower H₂ production. C. pasteurianum in NH₄ ⁺ limitation showed higher fermentation rates thanC. butyricum and a stabilized H₂ production around 2.08 (±0.06) mol per mol glucose consumed at various defined pH conditions, although the acetate/butyrate ratio increased to 1 at pH 7.0. The latter was also observed in phosphate-limitation, but here H₂ production was maximal (1.90 mol. per mol glucose consumed) at the lowest pH (5.5) tested.     

Influence of oxygen transfer rate and media composition on fermentation ofd-xylose byPichia stipitis NRRL Y-7124

Summary The optimization of ethanol production byPichia stipitis NRRL Y-7124 was analysed by ATP balance. Ethanol volumetric productivity was maximal (0.5–0.6 g/l h) only over a narrow range of oxygen transfer rates (3–5 mmol O₂/l h). Trace element supplements increased ethanol volumetric productivity 20%. Biotin and thiamine did not significantly affect ethanol yield. Vitamins and trace elements were not synergistic. Organic nitrogen source from yeast extract was used for growth simultaneously to ammonia.     

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.     

Influence of dilution rate on the morphology and technological properties ofLactobacillus delbrueckii subsp.bulgaricus

Lactobacillus delbrueckii subsp.bulgaricus ATCC 11842 was grown in a chemostat at 45°C and pH 5.5 using glucose as the carbon source, with the aim of optimizing biomass production. Cells were grown in a complex medium under nitrogen. At dilution rates lower than 0.18h^–1, it was difficult to keep steady-state conditions and pleomorphic forms were observed. The addition of 30mM Ca²⁺ and Mn²⁺ reverted the cells to normal shape: 30mM Mg²⁺ had no effect. Increasing the dilution rate resulted in normal morphology without the addition of any cations. Under these conditions, a maximum productivity of 1.24g dry biomass 1^–1 h^–1 was obtained. The maximum growth yield, corrected for maintenance, was 30g biomass mol^–1 glucose and the maintenance energy was 0.26g glucose g^–1 biomass h^–1. Lactate was the main fermentation product at all glucose concentrations used in the fed medium. Cells grown at high dilution rates had normal technological properties (acid production and proteolysis) when tested in milk.     

Effects of culture conditions on the co-fermentation of a glucose and xylose mixture to ethanol by a mutant of Saccharomyces diastaticus associated with Pichia stipitis

Substrates that contain hexose as well as pentose sugars can form an interesting substrate for the production of ethanol. Pichia stipitis and a respiratory-deficient mutant of Saccharomyces diastaticus were used to convert such a substrate into ethanol under continuous culture conditions. With a sugar mixture (glucose 70%/xylose 30%) at 50 g/l, the xylose was entirely consumed when the dilution rate (D) did not exceed 0.006 h^–1 whereas the glucose was entirely consumed whatever the D. The study of influence of initial substrate concentration (S₀) was performed at D = 0.015 h^–1. Under these conditions the substrate was entirely consumed when its initial concentration did not exceed 20 g/l. With S₀ = 80 g/l the residual xylose concentration reached 20.5 g/l. At low D or at low S₀, P. stipitis was the dominant species in the fermentor. Increasing the D or S₀ resulted in the wash-out of P. stipitis mainly because of its low ethanol tolerance. Correspondence to: J. P. Delgenes     

Growth of a Catharanthus roseus cell suspension culture in a modified chemostat under glucose-limiting conditions

Summary A system for the continuous cultivation of plant cells has been developed, based on a commercially available 3–1 turbine-stirred fermentor. A special device was constructed to provide for homogeneous effluent from the culture at low dilution rates. Two steady states with Catharanthus roseus cells growing under glucose limitation are described with respect to biomass yield on the carbon and energy source glucose, specific oxygen consumption, specific carbon dioxide production and (by)product formation. From a carbon balance for each steady state it is shown that the flow of carbon to the culture (as glucose) practically equalled the flow of carbon from the culture (as biomass, carbon dioxide and (by)product). Biomass yields on glucose were 0.31 g/g and 0.35 g/g at dilution rates of 0.0060 l/h and 0.0081 l/h respectively. The striking difference between the obtained yield coefficients and biomass yield commonly found for batch-cultured plant cells is discussed.     

Glycerol production by semicontinuous fed-batch fermentation with immobilized cells of Saccharomyces cerevisiae

Summary Semicontinuous fed-batch glycerol fermentations with Saccharomyces cerevisiae cells immobilized in sintered glass Raschig rings were carried out in fixed-bed loop reactors with a working volume of either 0.8 l or 8 l. The influence of biomass, temperature and CO₂ gassing on the glycerol yield was examined. The highest glycerol yield of 85 g l^–1 was achieved at 30° C and average CO₂ gassing rate of 0.4 v/v m with a theoretical glycerol yield of 67%. Fed-batch fermentations with free cells indicated an inhibition mechanism of the glycerol produced, affecting the fermentation capacity of the yeast strain used.Offprint requests to: H.-J. Rehm