Analysis of noise and bias in fermentation oxygen uptake rate data

The calculation of many derived fermentation variables such as the respiratory quotient (RQ) and mass transfer coefficient (K(L)a) requires the differences between the molar percentages of oxygen and carbon dioxide in the fermentor inlet and exit gas, called the %OUR and %CER. Noise and bias in %CER data is of order that in the exit gas carbon dioxide analysis. However, the relative amount of noise in the %OUR is one to two orders of magnitude greater than the noise in the raw oxygen analyses because the %OUR is calculated as a small difference between two large quantities. The noise in the %OUR is white with a Gaussian amplitude probability distribution of absolute standard deviation 0.0145. A chi-square filter of the %OUR data is shown to considerably improve the quality of the calculated RQ and K(L)a for a fermentation of Streptomyces clavuligerus. (c) 1992 John Wiley & Sons, Inc.     

Effect of RQ and pre-seed conditions on biomass and galactosyl transferase production during fed-batch culture of S. cerevisiae BT150

A feedback RQ controlled fed-batch process for the recombinant production of a soluble human N-deglycosylated recombinant beta-1, 4-galactosyltransferase (NdrGal-T) with Saccharomyces cerevisiae BT150 was investigated. Several RQ values were tested for optimal production of NdrGal-T. Four times higher volumetric activity was reached at RQ=1.0 (32 U l(-1)) than at all higher RQ values (about 8 U l(-1)). RQ, 1.0 was the best choice for both, biomass and enzyme production. Optimal concentration of glucose in preculture was 25 g l(-1). At higher values slightly more ethanol was produced than at lower values of preculture glucose concentrations, moreover no positive effect on biomass and enzyme production was found. Lower values caused not only decrease of ethanol but also decrease of biomass formation (from 1.69 g h(-1) to 0.81 g h(-1)) and enzyme overall productivity (from 2.2 U h(-1) to 0.63 U h(-1)). Successfully performed cultivation with three precultures predicted scale-up possibility of feedback RQ-controlled NdrGal-T production with S. cerevisiae BT150 from lab to pilot-scale fermentor.     

Effect of changes in the pH and carbon dioxide evolution rate on the measured respiratory quotient of fermentations

The total concentration of dissolved carbon dioxide in fermentation broths is one to two orders of magnitude greater than that of oxygen for pH > 6.5. The rate of change in this total concentration can be sufficiently large to produce a discrepancy between the carbon dioxide transfer rate (CTR) across the gas-liquid interface, available from gas analyses, and the carbon dioxide evolution rate (CER) of biomass in the fermentor. The CER is the variable of most interest to fermentation technologists but cannot be measured directly. The CTR is commonly used to yield the measured respiratory quotient (called here the TQ, or transfer quotient). Evaluation of the real underlying respiratory quotient (RQ), however, requiures the unmeasureable CER. Equations defining the problem are presented and are found to accurately predict the discrepancy between the TQ and the RQ in fed-batch fermentations of Escherichia coli. During the exponential growth phase, the TQ is less than the RQ. A changing pH can cause the TQ to be bigger or smaller than the RQ, while pH fluctuations associated with on-off pH controller action make the CTR and hence the TQ noisy. The RQ is estimated on-line during an E. coli fermentation and is shown to be constant during the fermentation, even though the TQ varies greatly. (c) 1992 John Wiley & Sons, Inc.     

Metabolic changes during substrate shifts in continuous cultures of the yeast Candida boidinii variant 60

Summary Substrate shift experiments in chemostat cultures with either methanol or glucose as carbon source were performed with the yeast Candida boidinii variant 60. At low dilution rates of 0.064 h^–1 the culture may be easily shifted from methanol to glucose medium and back again to methanol. From these experiments it can be seen that glucose does not give rise to any catabolite inhibition of alcohol oxidase. Alcohol oxidase and formaldehyde dehydrogenase seem to be regulated by a repression-derepression mechanism, as small basal activities of both these enzymes can still be measured during growth on glucose. On the other hand, formate dehydrogenase activity is completely absent in the presence of glucose. This kind of regulation seems to favor the smooth switch from growth on glucose to methanol metabolism.With methanol or glucose, growth yields (Y_S) of 0.3 and 0.35, respectively may be obtained, and oxygen consumption (Q_{O 2}) is much higher in methanol cultures than in glucose-grown cells. Accordingly, the RQ values during growth on methanol decrease to about 0.5. Based on the yield coefficient of 0.3, it is possible to calculate that 38% of the methanol consumed must be incorporated into biomass, whereas 62% of the methanol is oxidized to CO₂. The corresponding RQ of 0.56 could not be experimentally ascertained.The activities of three mitochondrial enzymes were found to be higher in methanol-grown cells than in cells from glucose cultures. The low activites of enzymes for the phosphogluconate route in methanol-grown cells indicates that a cyclic oxidation of formaldehyde via hexose phosphate to CO₂ cannot be of great importance for methanol metabolism.List of Symbols D 1/h Dilution rate - 1/h Specific growth rate - Q_{CO 2} mmol/g·h Specific CO₂ production rate - Q_{O 2} mmol/g·h Specific O₂ comsumption rate - Q_S g/g·h Specific substrate consumption rate - RQ ./. Respiratory quotient (Q_{CO 2}/Q_{O 2}) - S_O g/l Substrate concentration in the feeding medium - $#x0073;$#x0304 g/l Substrate concentration in the fermentor - $#x0078;$#x0304 g/l Biomass in the fermentor - Y_{O 2} g/mmol O₂ Biomass yield on oxygen - Y_S g/g Biomass yield on carbon source     

Inhibitory effect of carbon dioxide on the fed-batch culture of Ralstonia eutropha: evaluation by CO2 pulse injection and autogenous CO2 methods

In order to see the effect of CO(2) inhibition resulting from the use of pure oxygen, we carried out a comparative fed-batch culture study of polyhydroxybutyric acid (PHB) production by Ralstonia eutropha using air and pure oxygen in 5-L, 30-L, and 300-L fermentors. The final PHB concentrations obtained with pure O(2) were 138.7 g/L in the 5-L fermentor and 131.3 g/L in the 30-L fermentor, which increased 2.9 and 6.2 times, respectively, as compared to those obtained with air. In the 300-L fermentor, the fed-batch culture with air yielded only 8.4 g/L PHB. However, the maximal CO(2) concentrations in the 5-L fermentor increased significantly from 4.1% (air) to 15.0% (pure O(2)), while it was only 1.6% in the 30-L fermentor with air, but reached 14.2% in the case of pure O(2). We used two different experimental methods for evaluating CO(2) inhibition: CO(2) pulse injection and autogenous CO(2) methods. A 10 or 22% (v/v) CO(2) pulse with a duration of 3 or 6 h was introduced in a pure-oxygen culture of R. eutropha to investigate how CO(2) affects the synthesis of biomass and PHB. CO(2) inhibited the cell growth and PHB synthesis significantly. The inhibitory effect became stronger with the increase of the CO(2) concentration and pulse duration. The new proposed autogenous CO(2) method makes it possible to place microbial cells under different CO(2) level environments by varying the gas flow rate. Introduction of O(2) gas at a low flow rate of 0.42 vvm resulted in an increase of CO(2) concentration to 30.2% in the exit gas. The final PHB of 97.2 g/L was obtained, which corresponded to 70% of the PHB production at 1.0 vvm O(2) flow rate. This new method measures the inhibitory effect of CO(2) produced autogenously by cells through the entire fermentation process and can avoid the overestimation of CO(2) inhibition without introducing artificial CO(2) into the fermentor.     

Production of single cell protein from rice polishings using Candida utilis

Microbial protein was produced from defatted rice polishings using Candida utilis in shake-flasks and a 14-l fermentor to optimize fermentation conditions before producing biomass in a 50-l fermentor. The organism supported maximum values of 0.224 h⁻¹, 0.94, 1.35, 1.75, 2.12 g l⁻¹ h⁻¹, 0.62 g cells g⁻¹ substrate utilized and 0.38 g g⁻¹ for specific growth rate, true protein productivity, crude protein productivity, cell mass productivity, substrate consumption rate, cell yield, crude protein yield, respectively in 50-l fermentor studies using optimized cultural conditions. Maximum values compared favourably or were superior to published data in literature. The biomass protein in the 50-l fermentor contained 22.3, 27.8, 19.2, 9.5, 38.12, 8.5 and 0.27% true protein, crude protein, crude fibre, ash, carbon, cellulose and RNA content, respectively. The dried biomass showed a gross metabolizable energy value of 2678 kcal kg⁻¹ and contained all essential and non-essential amino acids. Yeast biomass as animal feed may replace expensive feed ingredients currently being used in poultry feed and may improve the economics of feed produced in countries like Pakistan. This revised version was published online in August 2006 with corrections to the Cover Date.     

Concentration-time curves in fed-batch fermentations followed by a batch phase

Summary A criterion is proposed to plot concentration-time curves in fed-batch fermentations when the reactor filling stage is followed by a batch phase.Nomenclature F mash feeding rate - R cells growth rate - S TRS concentration in the feeding mash - t time - T time measured from the beginning of the feeding phase until to the end of the fermentation - TRS total reducing sugars, calculated as glucose - X cells concentration (dry matter) - fermentor filling-up time     

Influence of exponentially decreasing feeding rates on fed-batch ethanol fermentation of sugar cane blackstrap molasses

Summary The ethanol yield was not affected and the ethanol productivity was increased when exponentially decreasing feeding rates were used instead of constant feeding rates in fed batch ethanol fermentations. The influences of the initial sugar feeding rate on the ethanol productivity, on the constant ethanol production rate during the feeding phase and on the initial ethanol production specific rate are represented by Monod-like equations.Nomenclature F reactor feeding rate (L.h^–1) - F_o initial reactor feeding rate (L.h^–1) - K time constant; see equation (l) (h^–1) - M_E mass of ethanol in the fermentor (g) - M_s mass of TRS in the fermentor (g) - M_x mass of yeast cells (dry matter) in the fermentor (g) - P ethanol productivity (g.L^–1.h^–1) - R ethanol constant production rate during the feeding phase (g.h^–1) - s standard deviation - S_o TRS concentration in the feeding mash (g.L^–1) - t time (h) - T fermentor filling-up-time (h) - T time necessary to complete the fermentation (h) - TRS total reducing sugars calculated as glucose (g.L^–1) - V_o volume of the inoculum (L) - V_f final volume of medium in the fermentor (L) - X_o yeast concentration of the inoculum (dry matter) (g.L^–1) - ethanol yield (% of the theoretical value) - initial specific rate of ethanol production (h^–1)     

Acetic acid production using a fermentor equipped with a hollow fiber filter module

The continuous production of acetic acid by Acetobacter aceti M23 was carried out using a fermentor equipped with a hollow fiber filter module. The culture continued for 830 h with various dilution rates, which were changed stepwisely from low to high. The final cell concentration was 21.9 g dry cell/L and the maximum productivity of acetic acid was 12.7 g/L.h for the exit acetic acid concentration of about 50 g/L. The productivity was higher than any literature's values surveyed so far. The cell concentration was 62.8 times and the productivity was 4.6 times as high as those of the fermentor without the filter module. The productivity increased with the increase of dilution rate up to 0.3 h(-1). It is interesting to note that the viable cell concentration was kept almost constant about 1.1 x 10(9) cells/ml in spite of the increase of dilution rate. Use of oxygen-rich air was indispensable to establish the high productivity of acetic acid.     

Estimating cell specific oxygen uptake and carbon dioxide production rates for mammalian cells in perfusion culture

We present robust methods for online estimation of cell specific oxygen uptake and carbon dioxide production rates (q(O2) and q(CO2), respectively) during perfusion cultivation of mammalian cells. Perfusion system gas and liquid phase mass balance expressions for oxygen and carbon dioxide were used to estimate q(O2), q(CO2) and the respiratory quotient (RQ) for Chinese hamster ovary (CHO) cells in perfusion culture over 12 steady states with varying dissolved oxygen (DO), pH, and temperature set points. Under standard conditions (DO = 50%, pH = 6.8, T = 36.5°C), q(O2) and q(CO2) ranges were 5.14-5.77 and 5.31-6.36 pmol/cell day, respectively, resulting in RQ values of 0.98-1.14. Changes to DO had a slight reducing effect on respiration rates with q(O2) and q(CO2) values of 4.64 and 5.47, respectively, at DO = 20% and 4.57 and 5.12 at DO = 100%. Respiration rates were lower at low pH with q(O2) and q(CO2) values of 4.07 and 4.15 pmol/cell day at pH = 6.6 and 4.98 and 5.36 pmol/cell day at pH = 7. Temperature also impacted respiration rates with respective q(O2) and q(CO2) values of 3.97 and 4.02 pmol/cell day at 30.5°C and 5.53 and 6.25 pmol/cell day at 37.5°C. Despite these changes in q(O2) and q(CO2) values, the RQ values in this study ranged from 0.98 to 1.23 suggesting that RQ was close to unity. Real-time q(O2) and q(CO2) estimates obtained using the approach presented in this study provide additional quantitative information on cell physiology both during bioprocess development and commercial biotherapeutic manufacturing.     

Patterns of aeration in a solid substrate fermentor through the study of the residence time distribution (RTD) of a volatile tracer

The injection of a volatile tracer in the gas flow allowed to describe the residence time distribution (RTD) in a solid substrate reactor. The chromatographic analysis of Dirac impulses of acetone led to identify the fermentor as a first-order rate system. The evolution of the time constant (lambda) of the system versus the gas flow rate gave a flow rate value that permitted a homogeneous aeration of the fermentor.     

Design and simulation of a fuzzy controller for fed-batch yeast fermentation

In baker's yeast fermentation, the process is non-linear and the response of the system to changes in glucose feeding has a very long delay time. Therefore, a conventional system can not give satisfactory results. In this paper, a fuzzy controller designed to control a fed-batch fermenter is presented. The fuzzy controller uses Respiratory Quotient (RQ) as a controller input and produces glucose feeding rate as control variable. The controller has been tested on a simulated fed-batch fermenter. The results show that the maximum yeast production is possible by keeping the specific growth rate (μ) and the glucose concentration (C _s) at preset values (μ _Cand C _s,c) and minimizing the ethanol production.     

Influence of linearly decreasing feeding rates on fed-batch ethanol fermentation of sugar-cane blackstrap molasses

Summary The ethanol yield was not affected and the ethanol productivity increased (10%) when linearly decreasing feeding rates were used instead of constant feeding rates in fed-batch ethanol fermentations.Nomenclature F reactor feeding rate (L.h^–1) - M_E mass of ethanol in the fermentor (g) - M_s mass of TRS in the fermentor (g) - M_x mass of yeast cells (dry matter) in the fermentor (g) - P ethanol productivity (g.L^–1.h^–1) - s standard deviation - S_o TRS concentration in the feeding mash (g.L^–1) - t time (h) - T fermentor filling-up time (h) - TRS total reducing sugars calculated as glucose (g.L^–1) - X_o yeast cells concentration (dry matter) in the inoculum (g.L^–1) - average ethanol yield (% of the theoretical value)     

Continuous high-ethanol fermentation from cane molasses by a flocculating yeast

Repeated-batch fermentation by a flocculating fusant, Saccharomyces cerevisiae HA 2, was done in a molasses medium that contained 20% (w/v) total sugar, at 30°C in an automatically controlled fermentor, and the effects of ethanol concentration on the specific growth rate and the specific production rate of ethanol were studied. Both the specific growth rate and the specific production rate of ethanol fell with increase of ethanol concentration, and there was a linear correlation between each rate and the concentration of thanol. The maximum specific growth rate (μ_max) and the maximum specific production rate of ethanol (q_max) were 0.12 h⁻¹ and 0.1 g ethanol/10⁹ cells·h, respectively. The specific growth rate and the specific production rate of ethanol fell to zero at ethanol concentration of 89 g/l and 95 g/l, respectively. The number of viable cells, calculated from the linear inhibition equation, was 1.3 × 10⁹ cells/ml for production of 85 g/l ethanol at a dilution rate (D₁) of 0.2 h⁻¹. Based on this estimation, a laboratory-scale continuous fermentation, using two fermentors in series, was done. In the second fermentor, 85 g/l ethanol was produced at a dilution rate (D₁) of 0.2 h⁻¹ by the active feedig of the fermented mash from the first fermentor into the second fermentor by pumping (hereafter called active feeding). To maintain the number of viable cells above 10⁹ cells/ml in the second fermentor, a active feeding ratio of more than 23% was required. Under these conditions, 81 g/l ethanol was produced in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹, and the high ethanol productivity of 20.3 g/l·h could be achieved. A bench-scale continuous fermentation, using two fermentors in series, with a active feeding ratio of 25% was done. An ethanol concentration of 84 g/l in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹ was achieved, just as it was in the laboratory-scale fermentation test.     

Time difference scanning gel chromatography: computer simulations

The time difference profile method of gel scanning chromatography developed by Brumbaugh, Saffen and Chun (Biophysical Chemistry, 1979) has been examined by computer simulation. The method is found to produce values for centroid movements that mimic those of the system being examined but are not quantitatively correct. In all cases the time differential "centroid" is larger than that of the concentration derivative (true) centroid and move at a rate slightly faster than the true centroids. This faster rate slowly decreases towards the true rate but does not approach it within reasonable times. This distorted movement reflects the distorted emphasis given to the larger species in the time differential method. The time difference method has been shown to give an adequate measure of the axial dispersion coefficient, L, for single species systems.     

Studies on on-line bioreactor identification. IV. Utilization of pH measurements for product estimation

Relationships between the total rate of biomass growth and the rate of ammonia addition to a fermentor for pH control are presented. These equations make use of the concept of reaction invariants and provide the additional information needed for bioreactor identification. They are especially useful when the RQ measurement is not sufficient for this purpose, such as when sensitivities arise with the measured values of the respiratory quotient or when fermentation products are formed. The cases of batch, fed-batch and continuous fermentations, forming products with or without acidic/basic properties are considered. The derived relationships were successfully tested with nonbiological acid-base continuous flow reaction systems and subsequently applied to the identification of the continuous yeast fermentation of glucose to ethanol. Results of these experimental studies are also presented.     

Orexins对小鼠摄食和能量代谢的影响

目的:探讨Orexins对小鼠摄食和能量代谢的影响。方法:将小鼠分为摄食组和代谢组,摄食组通过中枢置管,注射不同剂量(1、3、10 nmol)的orexin-A和orexin-B,观察它们对小鼠摄食以及肝柠檬酸合酶活性的影响。代谢组将小鼠置于代谢笼内,通过中枢注射orexin-A,观察小鼠在光照条件、黑暗条件、禁食条件下呼吸商和代谢率的变化。结果:与对照组相比,1 nmol和10 nmol orexin-A在注射后4小时内可显著刺激小鼠进食(P0.05),而3 nmol orexin-A对摄食量的影响并不明显,但能显著促进柠檬酸合酶活性。任何剂量的orexin-B对小鼠摄食都没有显示出刺激作用(P0.05)。在光照条件下,orexin-A可显著降低呼吸商(RQ),代谢率显著升高(P0.05);而在黑暗条件下,orexin-A对RQ没有任何影响,但代谢率显著升高(P0.05);但是给禁食小鼠中注射orexin-A可诱导RQ的短暂升高,代谢率显著升高(P0.05)。结论:Orexins对小鼠摄食与能量代谢可能有一定的调控作用。     

Effects of palmitate and oleate on the respiratory quotient during acute feeding

Objective: Using tracers, we showed, over 9 hours, that palmitic acid (PA) is oxidized at a lower rate than oleic acid (OA). Our subsequent clinical trial showed that enriching the diet for 28 days with PA, relative to OA, lowered fatty acid (FA) oxidation. However, because this conclusion was based on indirect calorimetry for 7 hours after a test meal, transient differences in the kinetics of oxidation of OA and PA could explain these results. Thus, we hypothesized that increasing PA vs. OA would decrease FA oxidation during the first day of feeding the diets. Research Methods and Procedures: A double‐masked trial was conducted in 20 adults, who, after a baseline diet, were randomized to one of two experimental formula diets: high (HI) OA (PA = 1.7% kcal, OA = 31.4% kcal; N = 11) or HI PA (PA = 16.8% kcal, OA = 16.4% kcal; N = 9). Respiratory quotient (RQ) was measured over the first 14 hours of feeding the experimental diets (7:00 am to 9:00 pm ). To determine whether these subjects were representative of the subjects in the previous trial, we assessed RQ 28 days after beginning either diet. Results: During the first 14 hours of feeding the diets, time (p = 0.026) but not diet group had an effect on the difference between the RQ post‐feeding and the fasting pre‐value. However, RQ in the fed state was significantly higher in the HI PA group after 28 days of feeding. Discussion: Chronically increasing dietary PA for 28 days, but not acute meal feeding, lowers total FA oxidation.     

Effect of CO2 absorption on the measurement of CO2 evolution rate in aerobic and anaerobic continuous cultures

A general and simple equation is presented to account for the effect of CO₂ absorption and the dissociation of carbonic acid in liquid on the measurement of the CO₂ evolution rate (QCO₂) of both anaerobic and aerobic continuous cultures. For aerobic cultures the same equation applies to the measurement of the respiratory quotient (RQ). The deviation of QCO₂ and RQ, calculated from gas-phase measurements, from their true values can be assessed with two parameters: one accounts for the influence of pH, resulting from dissociation of carbonic acid, the other for the influence of operating conditions. Plots are given to show the influences of culture and operating conditions; they may be used as a guideline for choosing proper operating conditions for a reliable measurement of CO₂ evolution rate and RQ value.Dedicated to Prof. Dr. Fritz Wagner on the occasion of his 65th birthday     

Induction effect of PO 2 during continuous yeast production from ethanol in a multistage tower fermentor

Summary The effect of the periodic variation of the partial pressure of oxygen in the aeration gas on biomass concentrations, ethanol conversion, yield and productivity during continuous cultivations of the yeast Candida utilis in a multistage tower fermentor was studied. The results were compared with those obtained under aeration conditions with a constant P_{O 2} in the aeration gas. The results demonstrated that, with the optimum P_{O 2} in the aeration gas, the aeration procedure with the periodic variation of P_{O 2} in the gas phase permitted achievement of the same process parameters as those under constant P_{O 2}. Using this new aeration procedure, the consumption of pure oxygen can be lowered by 55% to 60%. In addition, the significance of the induction effect of P_{O 2} on growth characteristics in the individual stages of the fermentor was proved.Symbols Ac Concentration of acetic acid (g/l) - i Number of stage - P_{O 2} Partial pressure of oxygen in the aeration gas (torr) - P_R Productivity of the fermentor (g cell dwt/l/h) - S_R Ethanol concentration in the feed (g/l) - S Ethanol concentration in the cultivation broth (g/l) - t Time of continuous cultivation (h) - X Cell dry weight concentration (g/l) - (Y_X/S)_W Yield of cell dry weight from ethanol for the whole fermentor (g cell dwt/g ethanol) - Concentration interval in which parameters varied during the long-term cultivation at constant constant P_{O 2}=263.5 torr in the aeration gas - ₁ Concentration interval in which parameters varied during the long-term cultivation before the increase of P_{O 2} in the aeration gas - ₂ Concentration interval in which parameters varied during the long-term cultivation immediately after the decrtease of P_{O 2} in the aeration gas - ₃ Concentration interval in which parameters varied during the long-term cultivation about 24 h after the decrease of P_{O 2} in the aeration gas - ₄ Concentration interval in which parameters varied during the long-term cultivation about 48 h after the decrease of P_{O 2} in the aeration gas