Optimization of culture conditions for the production of an extracellular ribonuclease by <Emphasis Type="Italic">Aspergillus niger</Emphasis> in a benchtop bioreactor

SummarySelf-directing optimization was successfully employed to determine the optimal combination of engineering parameters, viz., pH, aeration rate and agitation rate, for extracellular ribonuclease production by Aspergillus niger SA-13-20 in a batch bioreactor. Maximal RNase production of 5.38 IU ml^–1 was obtained at controlled pH of 2.33, aeration rate of 1.67 v/v/m and agitation rate of 850 rev/min. The effect of oxygen on the fermentation was also investigated. With increase in volumetric oxygen transfer coefficients (K_La), cell growth and RNase production first increased and then decreased. RNase production was further increased to 7.10 IU ml^–1 and the fermentation time was shortened from 96 to 72 h by controlling dissolved oxygen concentration at 10% saturation by aerating oxygen after about 28 h of fermentation under the above optimal condition. The kinetic model showed that RNase production by A. niger SA-13-20 was growth-associated.     

Thermostable cellulases from <Emphasis Type="Italic">Streptomyces</Emphasis>sp.: scale-up production in a 50-l fermenter

Thermostable cellulase was produced by Streptomyces sp. T3-1 grown in a 50-l fermenter. Maximum cellulase activity was attained on the fourth day when agitation speeds and aeration rates were controlled at 300 rpm and 0.75 vvm, respectively. Maximum enzyme activities were: 148 IU CMCase ml^–1, 45 IU Avicelase ml^–1, and 137 IU -glucosidase ml^–1 with productivity of 326 IU l^–1 h^–1, which were 10--32% higher than the values obtained in shake-flask culturesRevisions requested 12 October 2004/1 November 2004; Received received 1 November 2004/14 December 2004     

Comparison of photobioreactors for cultivation of Undaria pinnatifida gametophytes

Undaria pinnatifida gametophytes were grown in 2.5 l bubble column and airlift reactor at 25 °C and light intensity of 40 mol m^–2 s^–1 for 6 days. With aeration at 1 l min^–1, the airlift reactor yielded higher growth rate (0.12 mg DW ml^–1 d^–1) than a bubble column (0.08 mg DW ml^–1 d^–1). The advantages were related to the more homogeneous fluid dynamic characteristics of the airlift reactor.     

Effects of initial maltose concentration, agitation and aeration rates on the production of glucosyltransferase byAspergillus niger CCRC 31494

Summary The microorganism Aspergillus niger CCRC 31494 can produce an extracellular glucosyltransferase (GTase, EC 2.4.1.24) with a high transglucosylating activity. The maximal enzyme production occurred at initial maltose concentration of 40 gl^-1. The microorganism was also grown in a 5-liter jar fermenter for GTase production. It was found that the optimal agitation and aeration rates were 750 rev min^-1 and 1.0 l min^-1, respectively, and the enzyme production was about 0.25–0.26 units ml^-1.     

Modelling continuous culture of Rhodospirillum rubrum in photobioreactor under light limited conditions

Rhodospirillum rubrum was grown continuously and photoheterotrophically under light limitation using a cylindrical photobioreactor in which the steady state biomass concentration was varied between 0.4 to 4 kg m^–3 at a constant radiant incident flux of 100 W m^–2. Kinetic and stoichiometric models for the growth are proposed. The biomass productivities, acetate consumption rate and the CO₂ production rate can be quantitatively predicted to a high level of accuracy by the proposed model calculations. Nomenclature: C _X, biomass concentration (kg m^–3) D, dilution rate (h^–1) Ea, mean mass absorption coefficient (m² kg^–1) I , total available radiant light energy (W m^–2) K, half saturation constant for light (W m^–2) R _W, boundary radius defining the working illuminated volume (m) r _X, local biomass volumetric rate (kg m^–3 h^–1) <r _X>, mean volumetric growth rate (kg m^–3 h^–1) V _W, illuminated working volume in the PBR (m^–3). Greek letters: , working illuminated fraction (–) _M, maximum quantum yield (–) bar, mean energetic yield (kg J^–1).     

Optimization of cell density and dilution rate in <Emphasis Type="Italic">Pichia pastoris</Emphasis> continuous fermentations for production of recombinant proteins

This paper provides an approach for optimizing the cell density (X_c) and dilution rate (D) in a chemostat for a Pichia pastoris continuous fermentation for the extracellular production of a recombinant protein, interferon (INF-). The objective was to maximize the volumetric productivity (Q, mg INF- l^–1 h^–1), which was accomplished using response surface methodology (RSM) to model the response of Q as a function of X_c and D within the ranges 150 X_c 450 g cells (wet weight) l^–1 and 0.1 _mD0.9 _m (_m=0.0678 h^–1, the maximum specific growth rate obtained from a fed-batch phase controlled with a methanol sensor). The methanol and medium feed rates that resulted in the desired X_c and D were determined based on the mass balance. From the RSM model, the optimal X_c and D were 328.9 g l^–1 and 0.0333 h^–1 for a maximum Q of 2.73 mg l^–1 h^–1. The model of specific production rate (, mg INF- g^–1 cells h^–1) was also established and showed the optimal X_c=287.7 g l^–1 and D=0.0361 h^–1 for the maximum (predicted to be 8.92×10^–3 mg^–1 g^–1 h^–1). The methanol specific consumption rate (, g methanol g^–1 cells h^–1) was calculated and shown to be independent of the cell density. The relationship between and (specific growth rate) was the same as that discovered from fed-batch fermentations of the same strain. The approach developed in this study is expected to be applicable to the optimization of continuous fermentations by other microorganisms.     

High density culture of the freshwater rotifer,Brachionus calyciflorus

The freshwater rotifer, Brachionus calyciflorus is one of the live food organisms used for the mass production of larval fish. In this study possibility of obtaining high density cultures of the freshwater rotifer B. calyciflorus were investigated. The two culture systems used differed in their air and dissolved oxygen supplies using three temperatures in each case: 24, 28 and 32 °C. Rotifers were batch-cultured using 5 l-vessels and fed with the freshwater Chlorella. The growth rate of rotifers significantly increased with an increase in temperature. The maximum density of the rotifers with air-supply at 24 °C, 6500 ind. ml^–1, was significantly lower than those cultured at 28 and 32 °C, i.e. 8600 and 8100 ind. ml^–1, respectively. Dissolved oxygen levels decreased with time and ranged from 0.8 to 1.4 mg l^–1 when the density of freshwater rotifer was the highest at each temperature. The highest density (19200 ind. ml^–1) of freshwater rotifer was obtained in cultures with a supply of oxygen at 28 °C. Densities of 13500 and 17200 ind. ml^–1 were found at 24 and 32 °C, respectively. Levels of NH₃-N increased with time and a dramatic increase of NH₃-N was observed at high temperatures. Levels of NH₃-N at 24, 28 and 32 °C were 13.2, 18.5 and 24.5 mg l^–1, respectively. These levels coincided with the highest rotifer density at each of the three temperatures. When rotifers were cultured with an oxygen-supply and pH was adjusted to 7, the maximum density of rotifer reached 33500 ind. ml^–1 at 32 °C . These results suggested that high density culture of freshwater rotifer, B. calyciflorus could be achieved under optimal conditions with DO value of exceeding 5 mg l^–1 and NH₃-N values of lower than 12.0 mg l^–1.     

Oxygen transfer on β- D-galactosidase production by Kluyveromyces marxianus using sugar cane molasses as carbon source

The optimal initial volumetric oxygen transfer coefficient (K_La) was 60 h^–1 for the production of -d-galactosidase from Kluyveromyces marxianus CDB 002, using sugar cane molasses as carbon source. At this K_La applying an agitation/aeration relationship of 700 rpm/0.66 vvm resulted in 812 U l^–1 h^–1 for -d-galactosidase production. This was about 50% better than a relationship of 500 rpm/2 vvm at the same K_La.     

Examining the relationship between bacteria and heterotrophic nanoflagellates in Funka Bay (Japan) using the size-fractionation method

The chemical and biological conditions, and the bacteria-heterotrophic nanoflagellate (HNF) relationship were investigated in the vicinity of Funka Bay, southwest of Hokkaido, Japan during early spring 1999. At the time of sampling, chlorophyll a concentration, bacteria, phycoerythrin rich-cyanobacteria, and HNF abundance were in the following ranges: 0.3–3.6 g l^–1, 2.5–5.6 × 10⁵ cells ml^–1, 0.6–1.2 × 10³ cells ml^–1, and 2.2–4.2 × 10³ cells ml^–1, respectively. Dissolved inorganic nitrogen, phosphate and silicate concentrations were in the ranges: 8.7–12.2 M, 0.9–2.0 M, and 21.6–25.5 M, respectively. Primary production ranged from 6.4 to 76.3 mg C m^–3 d^–1. Using water samples from regions of different productivity levels (in and outside bay), the bacteria - HNF relationship was uncoupled experimentally by the size-fractionation technique. Higher primary production (19.9 mg C m^–3 d^–1) in the bay supported higher bacterial growth rate (0.029 h^–1). However, outside the bay both primary production (6.4 mg C m^–3 d^–1) and bacterial growth rate (0.007 h^–1) were lower. The HNF growth rates and grazing rates were similar for both but by comparing both HNF grazing capacity and bacterial production, there was net decrease in bacterial abundance outside the bay and net increase inside the bay. The microbial parameters (rates and abundance) and the amount of carbon flow estimated through the phytoplankton – dissolved organic matter (DOM) – bacteria loop were different between the coastal station and the open ocean station. However HNF grazing and growth rates was similar for both stations.     

Influence of agitation and aeration on growth and antibiotic production by <Emphasis Type="Italic">Xenorhabdus nematophila</Emphasis>

The effect of agitation and aeration on the growth and antibiotic production by Xenorhabdus nematophila YL001 grown in batch cultures were investigated. Efficiency of aeration and agitation was evaluated through the oxygen mass transfer coefficient (K _L a). With increase in K _L a, the biomass and antibiotic activity increased. Activity units of antibiotic and dry cell weight were increased to 232 U ml⁻¹ and 19.58 g l⁻¹, respectively, productivity in cell and antibiotic was up more than 30% when K _L a increased from 115.9 h⁻¹ to 185.7 h⁻¹. During the exponential growth phase, DO concentration was zero, the oxygen supply was not sufficient. So, based on process analysis, a three-stage oxygen supply control strategy was used to improved the DO concentration above 30% by controlling the agitation speed and aeration rate. The dry cell weight and activity units of antibiotic were further increased to 24.22 g l⁻¹ and 249 U ml⁻¹, and were improved by 24.0% and 7.0%, compared with fermentation at a constant agitation speed and a constant aeration rate (300 rev min⁻¹, 2.5 l min⁻¹).     

Chromate tolerance in strains of Rhodosporidium toruloides modulated by thiosulfate and sulfur amino acids

Cr(VI) tolerance was studied in four strains of Rhodosporidium toruloides and compared with that of a fifth strain, DBVPG 6662, isolated from metallurgical wastes and known to be Cr(VI) resistant. Tolerance was studied in relation to different species of sulfur (sulfates, thiosulfates, methionine, cysteine) at different concentrations. Djenkolic acid, a poor source of sulfur and an activator of sulfate transport, was also considered. In synthetic medium all strains except the Cr(VI)-resistant one started to be inhibited by 10 g ml^– (0.2 mm) Cr(VI) as K₂Cr₂O₇. DBVPG 6662 was inhibited by 100 g ml^– (2.0 mm) Cr(VI). In Yeast Nitrogen Base without amino acids (minimal medium), supplemented with varying concentrations of chromate, all Cr(VI)-sensitive strains accumulated concentrations of total chromium (from 0.8 to 1.0 g mg^– cell dry wt) after 18 h of incubation at 28 °C. In minimal medium supplemented with 10 g ml^– Cr(VI), the addition of sulfate did not significantly improve the yeast growth. Cysteine at m levels increased tolerance up to 10 g ml^–, whereas methionine only reduced the Cr(VI) toxicity in the strain DBVPG 6739. Additions of djenkolic acid resulted in increased Cr(VI) sensitivity in all strains. The best inorganic sulfur species for conferring high tolerance was thiosulfate at concentrations up to 1 mm. In all cases increased Cr(VI) tolerance was due to a significantly reduced uptake in the oxyanion by the cells and not to the chemical reduction of Cr(VI) to Cr(III) by sulfur compounds.     

The relative importance of different ciliate taxa in the pelagic food web of lake constance

Abundance, biovolume, and species composition of pelagic ciliates in Lake Constance were recorded over two annual cycles (1987/88). Production was estimated from mean annual biovolumes and size-specific growth rates obtained from the literature. Cell concentrations and biovolumes ranged from 0.1 to 120 cells ml^–1 and from 3 to 1,200 mm³ m^–3, respectively. Mean annual values were, respectively, 6.8 cells ml^–1 and 94 mm³ m^–3 in 1987, and 12.0 cells ml^–1 and 130 mm³ m^–3 in 1988. In both years, prostome nanociliates (<20m) dominated numerically, while strobiliids in the size range 20–35m contributed most significantly to ciliate production. Ciliate community production, according to a crude calculation, yielded approximately 10–15 g C m^–2 year^–1.     

Optimisation of agitation and aeration in fermenters

The problem of optimising agitation and aeration in a given fermenter is addressed. The objective function is total electric power consumed for agitation, compression and refrigeration. The major constraint considered is to ensure that the dissolved oxygen concentration is above the critical value. It is shown that it is possible to analytically calculate the optimal pair (air flowrate, stirrer speed) and that, at least for the industrial antibiotics fermentation used as case-study, the optimum lies within a window for satisfactory operation, limited by other possible constraints to the problem. Savings achievable by optimal operation as compared with current industrial procedure were found to be around 10% at pilot plant scale (0.26 m³) and 20% at full scale (85 m³).List of Symbols A fermenter cross sectional area (m²) - C dissolved oxygen concentration (mole m^–3) - C ^* DO concentration in equilibrium with the gas (mole m^–3) - C _crit critical DO concentration (mole m^–3) - C _p specific heat of air at constant pressure (J kg^–1 K^–1) - C _sp dissolved oxygen set point (mole m^–3) - C _v specific heat of air at constant volume (J kg^–1 K^–1) - D agitator diameter (m) - f pressure correction of air flow-rate - (Fl _g)_F aeration number at flooding - (Fr _g)_F froude number at flooding - k coefficient in expression for mass transfer coefficient - K _La volumetric oxygen transfer coefficient (s^–1) - m power exponent in expression for mass transfer coefficient - n gas flow rate exponent in expression for mass transfer coefficient - n ^* number of impellers - N rotation speed (s^–1) - N _F rotation speed at flooding (s^–1) - N _p unaerated power number - N _pg aerated power number - OUR Oxygen Uptake Rate (mole m^–3 s^–1) - p ₀ atmospheric pressure (N m^–2) - p ₁ compressor exit pressure (N m^–2) - p ₂ pressure at the bottom of the fermenter (N m^–2) - p ₃ pressure at the top of the fermenter (N m^–2) - P _c compression power (W) - P _d power added by expansion (W) - P _ev power removed by evaporation (W) - P _g agitation power (W) - P _m power added by metabolism (W) - P _r power removed by refrigeration (W) - P _t total power (W) - Q air flow-rate at atmospheric conditions (m³ s^–1) - Q _f air flow-rate at average fermenter conditions (m³ s^–1) - s ₀ absolute humidity at atmospheric conditions - s ₃ absolute humidity at fermenter exit - T tank diameter (m) - V liquid volume (m³) - v _s gas superficial velocity (m s^–1) - _i parameter defined in the text - safety margin for dissolved oxygen (mole m^–3) - ratio of specific heats of air - _g agitation efficiency - _c compression efficiency - _r refrigeration efficiency - liquid density (kg m^–3) - _g air density (kg m^–3) - latent heat of vaporisation of water (J kg^–1) The authors are grateful to Elsa Silva, Carlos Lopes, Carlos Aguiar, Fernando Mendes, and Alexandre Cardoso, who helped with parts of this work, and to CIPAN for permission to publish these data.     

Isolation and characterization of α-amylase derived from starchgrownClostridium acetobutylicum ATCC 824

Summary An extracellular -amylase was purified to homogeneity from the culture supernatant ofClostridium acetobutylicum ATCC 824 grown in synthetic medium containing starch by using a combination of ammonium sulfate fractionation, anion exchange chromatography and HPLC-gel filtration. The molecular weight of the 160-fold purified -amylase was determined by SDS-PAGE to be 61 kDa. HPLC analysis of end-products of enzyme activity on various substrates indicated that the enzyme acted specifically in an endo-fashion on the -1,4-glucosidic linkages. Enzyme activity was optimal over a pH range of 4.5–5.0 and temperature of 55°C, but was rapidly inactivated at higher temperatures. Addition of calcium chloride (2–5 mM) increased -amylase activity by ca. 20%, while the addition of 19 g ml^–1 of acarbose (a differential inhibitor of amylases) resulted in 50% inhibition. TheV _max andK _m of -amylase were 2.17 mg min^–1 and 3.28 mg ml^–1 on amylose, and 1.67 mg min^–1 and 1.73 mg ml^–1 on soluble starch, respectively.     

Action potentials inAcetabularia: Measurement and simulation of voltage-gated fluxes

Summary Amounts and temporal changes of the release of the tracer ions K⁺ (⁸⁶Rb⁺),²²Na⁺, and³⁶Cl^– as well as of H⁺ in the course of action potentials inAcetabularia have been recorded. New results and model calculations confirm in quantitative terms the involvement of three major ion transport systemsX in the plasmalemma: Cl^– pumps, K⁺ channels, and Cl^– channels (which are marked in the following by the prefixes,P, K andC) with their equilibrium voltages _X V _e and voltage/time-dependent conductances, which can be described by the following, first approximation. Let the maximum (ohmic) conductance of each of the three populations of transporter species be about the same (_P L, _KL,_C L=1) but voltage gating be different: the pump ( _{p V e} about –200 mV) being inactivated (open,oclosed,c) at positive going transmembrane voltages,V _m; the K⁺ channels (_K V _e about –100 mV) are inactivated at negative goingV _m; and the Cl^– channels (_C V _e: around 0 mV), which are normally closed (c) at a restingV _m (near_PV_e) go through an intermediate open (o) state at more positiveV _m before they enter a third shut state (s) in series. Model calculations, in which voltage sensitivities are expressed by the factorf=exp(V _mF/(2RT)), simulate, the action potential fairly well with the following parameters (_PK_co10/f ks^–1,_PK_oc1000·f ks^–1,_KK_co200·f ks^–1,_Kk_oc2/f ks^–1,_cK_co500·f ks^–1,_CK_oc5/f ks^–1,_CK_so0.1/f ks^–1,_Ck_os20·f ks^–1). It is also shown that the charge balance for the huge transient Cl^– efflux, which frequently occurs during an action potential, can be accounted for by the observation of a corresponding release of Na⁺.     

Conditions for open-air outdoor culture of Dunaliella salina in southern Spain

The optimization of the operation, under the climatic conditions of southern Spain, of an experimental plant for -carotene production by Dunaliella has been pursued. The effects of mixing, culture depth, cell density and dilution cycles on -carotene and biomass productivity were studied under a semicontinuous culture regime in open tanks outdoors. Using 3 m²-surface containers, the highest productivity values, for both -carotene and biomass, were recorded with a flow rate of 0.55 m s^–1; 10 cm depth; 0.7 – 0.9 × 10⁶cell ml^–1, population density; and dilution cycles of two days. An average annual productivity of 1.65 g (dry wt) m^–2 d^–1 was estimated for Dunaliella biomass, being that for -carotene of about 0.1 g m^–2 d^–1. Under these optimized conditions, experiments have been carried out at the Cadiz Bay with 20 m²-surface tanks during a whole-year cycle. The results obtained have validated this location and the operating conditions established as being most appropriate for efficient mass production of -carotene rich D. salina.     

Modeling of the pyruvate production with<Emphasis Type="Italic"> Escherichia coli</Emphasis> in a fed-batch bioreactor

A family of 10 competing, unstructured models has been developed to model cell growth, substrate consumption, and product formation of the pyruvate producing strain Escherichia coli YYC202 ldhA::Kan strain used in fed-batch processes. The strain is completely blocked in its ability to convert pyruvate into acetyl-CoA or acetate (using glucose as the carbon source) resulting in an acetate auxotrophy during growth in glucose minimal medium. Parameter estimation was carried out using data from fed-batch fermentation performed at constant glucose feed rates of q_VG=10 mL h^–1. Acetate was fed according to the previously developed feeding strategy. While the model identification was realized by least-square fit, the model discrimination was based on the model selection criterion (MSC). The validation of model parameters was performed applying data from two different fed-batch experiments with glucose feed rate q_VG=20 and 30 mL h^–1, respectively. Consequently, the most suitable model was identified that reflected the pyruvate and biomass curves adequately by considering a pyruvate inhibited growth (Jerusalimsky approach) and pyruvate inhibited product formation (described by modified Luedeking–Piret/Levenspiel term).List of symbols c_A acetate concentration (g L^–1) - c_A,0 acetate concentration in the feed (g L^–1) - c_G glucose concentration (g L^–1) - c_G,0 glucose concentration in the feed (g L^–1) - c_P pyruvate concentration (g L^–1) - c_P,max critical pyruvate concentration above which reaction cannot proceed (g L^–1) - c_X biomass concentration (g L^–1) - K_I inhibition constant for pyruvate production (g L^–1) - K_I^A inhibition constant for biomass growth on acetate (g L^–1) - K_P saturation constant for pyruvate production (g L^–1) - K_P inhibition constant of Jerusalimsky (g L^–1) - K_S^A Monod growth constant for acetate (g L^–1) - K_S^G Monod growth constant for glucose (g L^–1) - m_A maintenance coefficient for growth on acetate (g g^–1 h^–1) - m_G maintenance coefficient for growth on glucose (g g^–1 h^–1) - n constant of extended Monod kinetics (Levenspiel) (–) - q_V volumetric flow rate (L h^–1) - q_VA volumetric flow rate of acetate (L h^–1) - q_VG volumetric flow rate of glucose (L h^–1) - r_A specific rate of acetate consumption (g g^–1 h^–1) - r_G specific rate of glucose consumption (g g^–1 h^–1) - r_P specific rate of pyruvate production (g g^–1 h^–1) - r_P,max maximum specific rate of pyruvate production (g g^–1 h^–1) - t time (h) - V reaction (broth) volume (L) - Y_P/G yield coefficient pyruvate from glucose (g g^–1) - Y_X/A yield coefficient biomass from acetate (g g^–1) - Y_X/A,max maximum yield coefficient biomass from acetate (g g^–1) - Y_X/G yield coefficient biomass from glucose (g g^–1) - Y_X/G,max maximum yield coefficient biomass from glucose (g g^–1) - growth associated product formation coefficient (g g^–1) - non-growth associated product formation coefficient (g g^–1 h^–1) - specific growth rate (h^–1) - _max maximum specific growth rate (h^–1)     

Fermentation ofCandida utilis for uricase production

Summary Conditions for the production of microbial uricase byCandida utilis were studied. For the selected strain, hypoxanthine proved to be the most effective inducer of uricase formation. The highest values of biomass as well as uricase activity in the mechanically agitated fermentor were obtained under the following conditions: 50 h, rotation impeller speed 7 s^–1, air flow rate 1.25×10^–5 m³s^–1, concentration of inducer 0.1%.List of symbols b width of baffle, m - c length of baffle, m - D diameter of cylindrical fermentor, m - d diameter of impeller, m - d ₁ diameter of impeller disc, m - Fr _m impeller Froud number - g gravitional acceleration, ms^–2 - H height of batch surface above bottom, m - H ₂ height of impeller disc above bottom, m - h height of impeller blade, m - Kp _g flow rate number - L length of impeller blade, m - N rotational speed of impeller, s^–1 - Re _m impeller Reynolds number - T time, h - V volume of batch, m³ - V _g air (gas) flow rate, m³s^–1 - x mass fraction of the dry matter of cells - x ₀ initial value of the mass fraction of the dry matter of cells - _r volume fraction of the dry matter of cells - <eta<₁ viscosity of pure liquid, Pa s - viscosity of batch (suspension of microbial suspension), Pa s - density of batch, kg m^–3     

Mathematical modeling of production of microbial lipids

As a part of the investigations on the microbial lipid production using the yeast Rhodotorula gracilis, CFR-1, kinetics of the biomass synthesis has been studied using shake flask experiments. Using a medium containing a carbon to nitrogen ratio of 701, the rates of biomass production were followed at different initial substrate concentrations in the range of 20–100 kg/m³. A logistic model was found to be reasonably adequate to describe the kinetics of the growth of biomass; the maximum specific growth rate of 0.105 h^–1 was applicable for substrate concentrations less than 60 kg/m³, which gave reasonable agreement between predicted and actual biomass concentration values.List of Symbols S ₀, X ₀ kg/m³ Initial concentrations of sugar, non lipid biomass respectively - X, X(t) kg/m³ Concentrations of non lipid biomass at any time t - dX/dt kg/(m³ · h) Rate of biomass growth - h^–1 Specific growth rate - _max h^–1 Maximum specific growth rate - K _s mol/dm³ Monods constant - X _max kg/m³ Maximum biomass reached in a run     

An energy cost minimizing strategy for fermentation dissolved oxygen control

A cost-minimizing mathematical model for on-line control of dissolved oxygen using agitation speed and aeration rate was developed. In pilot scale monensin fermentation using Streptomyces cinnamonensis, this algortihm provided stable control of dissolved oxygen at 40%, reducing energy usage 27.8%. The agitation and aeration profiles provided by the algorithm respresent the pathway of least energy cost for control at the desired dissolved oxygen level. Other observed advantages of bivariable control were reduction of foaming, evaporation, and gas holdup. Reduced maintenance of compressors and agitator motors could also be expected due to decreased load. Monensin productivity equivalent to fermentation with constant agitation and aeration was not obtained, however, with potency reduced 14.8% with the dissolved oxygen control strategy.List of Symbols A m² cross sectional area of fermentor - A ₁, A ₂, A ₃, A ₄ constants of polynomial fit to Calderbank's equations - BP N/m² gauge back pressure - C _ag $/W/s cost of electrical power - C _Q $/m³ cost of compressed air - CE mol/m³/s carbon dioxide evolution rate - D m impeller diameter - DO, DO _meas, DO _sp % dissolved oxyen saturation at any time, measured, and setpoint respectively - h m height of liquid in fermentor - H N/m²/mmol Henry's constant for oxygen in water - H _av average gas holdup in fermentor - k _L a, k _L a _meas, k _L k _sp s^–1 oxygen mass transfer coefficient at any time, measured, and setpoint respectively - N, N _sp s^–1 agitation speed at any time and setpoint respectively - N _a, N _{a, sp} aeration number at any time and setpoint respectively - N _i total number of impellers - N _p impeller power number - N _s number of impellers into which air is directly sparged - OU, OU _meas mol/m³/s Oxygen uptake rate at any time and measured respectively - P W ungassed agitation power - P _g, P _g,meas, P _g,sp W gassed agitation power at any time, measured, and set point respectively - Q, Q _meas, Q _sp m³/s aeration rate at any time, measured, and setpoint respectively - T K fermentation temperature - u _g m/s linear gas velocity - V m³ fermentation liquid volume - mole fraction of oxygen in fermentation off-gas - calculation constant - motor efficiency - $/s sum of agitation and aeration costs - kg/m³ liquid density