repair manual for isuzu qt 23

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To add our e-mail address ( ), visit the Personal Document Settings under Preferences tab on Amazon. It has a novel format by having It's available on There are a lot of real-life exam Unless the culture produces a highly viscous extracellular product such as gum, it is also reasonable to assume that the viscosity of liquid in the fermenter is the same as that of water. Answer: (ii) 2.11 Mass and weight From the definition of density in Section 2.4.1, mass is equal to density multiplied by volume. For gases at low pressures, this means 21 mol O2 and 79 mol N2. Answer: 584 ppm, assuming that the density of the solution is equal to the density of water. 2.19 Gas composition Gas compositions are expressed as volume (Section 2.4.5). For relatively light gases such as oxygen, carbon dioxide, ammonia and nitrogen, we can assume that the ideal gas law is valid over the range of conditions applying to bioreactor operation (Section 2.5). This means that the relative partial volumes of the component gases will not change with temperature and pressure, so that the gas composition will be unaffected. The amount lost is therefore 72. From the reaction stoichiometry, 8 mol of nitrate are required for every 5 mol of acetic acid consumed. Answer: Nitrate (d) The conversion is based on the amount of limiting substrate available. From (c), nitrate is the limiting substrate and 5.95 mM of nitrate is available for the denitrification reaction. This small standard error indicates that the reliability of the mean is high. Answer: No, it falls outside of the 95 confidence interval 3.5 Measurement accuracy (a) The calculations shown can also be performed using computer or calculator software. http://www.paginemarxiste.it/userfiles/cyrus-8-amplifier-manual.xml repair manual for isuzu qt 23, repair manual for isuzu qt 235, repair manual for isuzu qt 230. Answer: Probe 2, because the standard deviation is higher (c) Because the standard error is smaller for Probe 1, this probe exhibits greater precision. If systematic errors are eliminated (Section 3.1.4), we can also say that Probe 1 is the more accurate probe. The results are listed and plotted below. Therefore, the straight line fit of the data cannot be considered a very good one. Answer: The straight line data fit is not very good because the residuals are not randomly distributed. 3.11 Nonlinear model: calculation of parameters (a) The proposed model equation has the general form of Eq. (3.16); therefore, if the model is suitable, a plot of. The data are plotted below. Krilliol concentration, s (g l-1) 10 1 0.1 0.0 0.5 1.0 1.5 2.0 2.5 Time, t (min) As the data give a straight line on semi-logarithmic coordinates, the model can be considered to fit the data well. The data are listed and plotted below. However, the non-linear model can be considered a better fit because the sum of squares of the residuals is smaller than for the linear model. The liquid-phase Cd concentration is reduced from 120 ppm to 25 ppm. The total mass of cell concentrate is denoted C; the total mass of buffer out is denoted B. The columns for water refer to water originating in the fermentation broth only: water in the buffer solution entering remains in the buffer solution leaving. For mass balancing, we need to convert this to a mass flow rate. Dichloromethane is abbreviated as DCM. The total mass of antibody solution in is denoted A; the total mass of pure dichloromethane in is denoted D; the total mass of mixture out is denoted M. Within M, let MPEG be the mass of PEG in the mixture stream. Because this problem requires an integral mass balance, the biomass remaining in the fermenter after 10 days of culture must also be included in the table even though it is not contained in any of the streams flowing into or out of the vessel. The In side of the mass balance table is complete. http://doingbusinessinargentina.com/userfiles/cyrus-cd8-service-manual.xml From Table C.1 (Appendix C), the molecular weight of monomeric starch is 162, the molecular weight of the biomass is 25.5, and the molecular weight of PHB is 86. If the concentration of PHB in the cells is 44, 44 g of PHB is produced for every 56 g of PHB-free biomass. If all the carbon in the substrate is converted into biomass, production of carbon dioxide is zero. Answer: Yes 4.23 Medium formulation A basis of 1 litre is used for the calculations. Therefore, with growth, the oxygen demand for acetic acid production is increased by 31. As the culture medium provides less glutamine than is required for consumption of all the glucose, glutamine is the limiting reactant and glucose is present in excess. These calculations show that the glucose and glutamine requirements for production of the maximum concentration of lactic acid are similar to those required for production of the maximum concentration of NH3. However, as indicated in the reaction equation in (a) for the overall metabolism of hybridoma cells, C from glucose and glutamine is also used for the production of by-products. The total mass of product is denoted P. The In side of the mass balance table is complete. Using a basis of 1 gmol of lactose, the n in this equation are the stoichiometric coefficients. The total mass of off-gas is denoted G; the total mass of product is denoted P. The In side of the mass balance table is complete. However, completion of the mass balance allows the calculations to be checked. The n in this equation are the moles of reactant or product involved in the reaction. Using a basis of 1 gmol of sucrose, the n in this equation are the stoichiometric coefficients. The n in this equation can be taken as the actual moles of reactants and products consumed or produced. The heat of reaction has fully oxidative and anaerobic components. From Table C.8 (Appendix C), glucose and fructose have the same molecular formula, C6H12O6, and the molecular formula for lysine is C6H14O2N2. https://ayurvedia.ch/boss-br-900cd-manual-download We can also check the consistency of the measured heat evolution data. The electron balance indicates that there must be an additional source of electrons in the culture that has not been taken into account in the calculations. This result is consistent with amino acids being used as an additional substrate during the initial culture period. FCA dt As F is also constant, the differential equation contains only two variables, CA and t. Separating variables gives: dC A. Separating variables and integrating:.Answer: 73 vegetable oil, 27 cod-liver oil 6.4 1. Drainage from mine tailings Flow sheet and system boundary These are shown in the figure below. The mass of substrate in the fermenter M is equal to Vs. The mass of substrate in the fermenter M is equal to Vs.Substituting parameter values into the equation. T ) ? U1 A1 (T ? Tair ) dt dT U 2 A2 (Tsteam. T ) dt dT U 2 A2 (Tsteam. Dh dt where h is the specific enthalpy of the water in the tank, which is the same as the specific enthalpy of the discharge stream. Answer: No 7.2 Rheology of fermentation broth (a) The rheogram is obtained by plotting shear stress. From the equation in Figure 7.8 for Casson plastic fluids, a plot of the square root of shear stress versus the square root of shear rate on linear coordinates gives a straight line if the fluid is a Casson plastic. Comparison of the residuals from the two models suggests that the equation for a pseudoplastic fluid is the better fit. The flow behaviour index continues to decrease until a cell concentration of about 12 is reached. These plots are shown below. It is unreasonable to expect to be able to provide this amount of power; the size of the motor and stirrer assembly required is impractical. Therefore, achieving turbulence with viscosity 1000 times greater than that of water is not possible. If the power draw of both impellers is reduced by the same percentage with gassing, the results of this comparison remain valid with gassing. https://eurodente.com/images/carver-dpl-20-manual.pdf Answer: The larger impeller. Although N P? and Di are greater for the larger impeller, a higher value for Di means that a much smaller Ni is required to avoid impeller flooding. However, if this turbine is operated with downward pumping, we can assume that it will flood at lower gas flow rates than a corresponding Rushton impeller (Section 8.4.3), all other geometric and operating parameters being equal. Therefore, we will perform the calculations for a Rushton turbine. Therefore, according to our assumption, the pitched-blade turbine will also be flooded. The vessel is operating virtually as a bubble column with little benefit being obtained from stirring in terms of mixing or gas dispersion. From (1), this can be expressed as. Therefore, we can say that: N JS2. As N P? depends on Di, we can write: P. N P? N JS3 Di 5 Substituting (1) into this equation: P. Di?2 (2) where Ni is the stirrer speed required for complete gas dispersion. In the turbulent regime, the relationship between P and Di is given by Eq. (8.9). Assuming that the percentage reduction in power with sparging is the same for Rushton turbines of different diameter, we can write: P. N P? N i3 Di 5 For complete gas dispersion, Ni depends on Di according to (2). The stirrer speed required for complete solids suspension is given by Eq. (8.18). For different impellers of the same size, all the terms in Eq. (8.18) remain constant except for S. Therefore, we can write: N JS. S In the turbulent regime without gassing, the equation for power as a function of operating conditions is Eq. (8.9). From Eq. (8.9), for complete solids suspension using different impellers of the same diameter we can write: P. N P? N JS3 Combining these equations gives: P. The power P in Eq. (8.22) did not change with gassing because the operating stirrer speed was increased.Therefore, from Eq. (8.22), the ratio of mixing times in the two fermenters is: tm2. This justifies application of Eqs (8.9) and (8.22) and N P? for the Rushton turbine. This justifies the application of Eqs (8.9) and (8.22) and N P? for the A315 hydrofoil impeller. To avoid having to modify the stirrer motor or drive assembly, impeller retrofitting is carried out so that the power draw and stirrer speed remain the same (Section 8.14). First, calculate the power draw for operation of the Rushton turbine at 150 rpm before retrofitting. The second assumption is not required if additional N P? values were available for different impeller:tank diameter ratios. Therefore, the cost of retrofitting is difficult to justify based on the expected mixing times. (c) (i) For future new fermenter installations without gassing, the hydrofoil impeller is likely to give the best mixing performance with strong axial velocities and low power consumption (Section 8.4.4, Hydrofoil Impellers subsection). Given the uncertainties associated with this criterion and the effective volume for dissipation of turbulence kinetic energy, we will use as a conservative approximation that. As gassing is provided through the reactor headspace, the culture liquid in the bioreactor is not sparged; therefore, there is no reduction in stirrer power due to gassing. Let us assume that flow is turbulent: this is checked below. As the value of N P? depends on the impeller:tank diameter ratio, we must first calculate DT. This justifies the application of Eq. (8.9) and N P?. Answer: 50 rpm (b) If the stirrer power is dissipated close to the impeller rather than throughout the vessel volume. There is a substantial difference between the answers obtained in (a) and (b). This illustrates the shortcomings of the Kolmogorov-scale approach for estimating the operating conditions required to avoid shear damage. Let us assume that flow in the bioreactor is turbulent: this is checked below. The flow diagram for cocurrent flow is shown below. The dimensionless numbers in this equation are Re, Pr and Nu. As fractional units are not available, four units must be purchased.Re is given by Eq. (9.28). The linear velocity of the fluid u is equal to the volumetric flow rate per tube divided by the inside cross-sectional area of the tube. Remax is given by Eq. (9.28) with D equal to the outer pipe diameter (Section 9.5.1, Flow at Right Angles to a Bank of Tubes without Phase Change subsection). Re is given by Eq. (9.28). The linear velocity of the fluid u is equal to the volumetric flow rate in the cooling coil divided by the inside cross-sectional area of the pipe,.The rate of shaft work W?s in Eq. (9.48) is the power dissipated by the impeller. The rate of shaft work W?s is equal to the power dissipated from the stirrer. Under these conditions, the stirrer power without gassing is evaluated using Eq. (8.7) with the value of NP dependent on Rei. The results for Q, s 1000 100 Q? W? s 10 ??H? rxn -1 (kJ s ) 1 0.1 0.4 5 1 10 Stirrer speed, Ni (s-1) (d). Therefore, the rate at which heat can be removed from the system Q? is increased. However, the rate at which heat is dissipated by the stirrer W?s also increases with stirrer speed. When the curves for Q? and W?s intersect, the entire heat transfer capacity of the fermenter cooling system is being used just to remove the heat generated by stirring; the system is unable to remove any of the heat generated from reaction. These results can be compared with the mass of cells.Similarly: 2 2 ( PT ) E. Answer: 40. This calculation illustrates the sensitivity of the oxygen balance method to the accuracy of the measured parameters used in Eq. (10.53). This sensitivity arises from the subtraction of two numbers of similar magnitude for the moles of oxygen in and out of the system. The effect of the electrode response time and boundary layers should be determined at a range of stirrer speeds using the techniques described in Section 10.10.2 (Electrode Response Time and Liquid Boundary Layers subsection). The effect of gas-phase dynamics should be tested using different methods of deoxygenation as described in Section 10.10.2 (Gas-Phase Dynamics subsection). Calculated values of. This suggests that boundary layer effects were eliminated at 50 rpm. As the kLa measurements were conducted at 60 rpm, we can conclude that significant boundary layers were not present during the measurement procedure. Because bubbles and gas hold-up are not involved in shakeflask aeration, gas-phase dynamics is not a significant issue in this case. Answer: 49 s, assuming that electrode and boundary layer effects are negligible (b) The closures have cylindrical geometry. The data after converting the units to s and m3 are listed and plotted below.The data after converting the units to s and m3 are listed and plotted below.These values are listed below. Therefore, a 2 error in measurement of the particle density results in a 61 error in the estimate of the maximum centrifuge throughput. Answer: The estimated maximum centrifuge throughput has an error of 61.Pressure (MPa) 57 89. The measured solubility results are listed and plotted below. Accordingly, considerable further processing of the precipitate is likely to be required to increase the product purity. This may be responsible for some deviation between the predicted and experimental antibody recoveries. In addition, solubility in protein mixtures such as culture broth is generally less than that predicted by the Cohn relationship, due to co-precipitation of other proteins (Section 11.8.2, Salting-Out subsection). Therefore, as the toxoid stays in the column for the shorter time, it must be the larger molecule. The average particle size Lav retained on each screen is calculated by taking the average of the aperture sizes of that screen and the one above it. From the graph above, LD ? 0.13 mm. Answer: 0.13 mm 11.33 Crystal growth and nucleation rates Aperture sizes for Tyler screens are given in Table F.2 in Appendix F. The increment in aperture size from above ?L is calculated from the aperture values. The mass of the crystals is represented as a slurry density (Section 11.12.1, Size Distribution subsection) to take into account the sample volume of 1 litre. Results calculated from the data provided are listed below. If the crystalliser is well mixed, the total mass of crystals per unit volume in the sieved sample taken from the vessel outlet is equal to the operating magma density. The discrepancy may be attributed to the strong dependence of the MSMPR equation on the fourth power of the slope obtained from the measured data. A relatively small variation in the slope obtained from fitting the data results in a large change in the calculated magma density. Rearranging the equation gives: 4 slurry density. Xc during drying, constant-rate drying applies. The mass of completely dry solid Ms is obtained from the cake volume and the density of the dry material. Therefore, the reaction at very low substrate concentrations can be expected to proceed at a significantly higher rate using the variant compared with the rat enzyme. The kinetic properties of the variant enzyme are therefore more suited for application to cancer patients. T is converted to kelvin using Eq. (2.27). The parameter values are listed and plotted below. Answer: With xylose as substrate, the catalytic efficiency of the enzyme is 6.7-fold greater than with glucose as substrate (b) From Section 12.3.3, catalytic efficiency is a measure of the substrate specificity of the enzyme. Therefore, this enzyme has a greater specificity for xylose as substrate than for glucose. Answer: The enzyme has a greater specificity for xylose as substrate compared with glucose 12.8 Effect of temperature on the hydrolysis of starch (a) The activation energy is determined using the Arrhenius equation, Eq. (12.22), with k equal to the initial rate of glucose production. T is converted to kelvin using Eq. (2.27). The parameter values are listed and plotted below.Answer: Yes (b) The equations for each of the straight lines in the plots in (a) are listed below. The data and calculations are tabulated below. The instantaneous biomass yield coefficients calculated using Eq. (12.108) and the values of rX from (a) are listed and plotted below. The mid-point slope method is used to determine growth rates from the biomass concentration data. Answer: Near the beginning of the culture (b) The mid-point slope method is used to determine the rate of substrate uptake as a function of time. This plot is shown below. 100 10 1 0 1 2 3 4 5 Time (days) The cell concentration data can be fitted with a straight line for only part of the culture period: exponential growth occurs between about 0.5 and 2.5 days. There is a lag phase before 0.5 days; after 2.5 days, the rate of cell growth declines. Answer: Yes (d), (e) The observed biomass yield from substrate is calculated using Eq. (12.78). As the measured data allow many values of ?X and ?ST to be determined, we can use a plot of ?X versus ?ST to estimate the yield. Using a basis of 1 litre and calculating ?X and ?ST as the difference between the measured values and the initial value of X or S, the results are listed and plotted below. The fit is reasonably good,.Therefore, growth is exponential at each of the temperatures tested. Answer: Yes; stationary phase occurs between about 7.5 h and 8.5 h (vii) As explained in Section 12.8.3, the transition from growth to stationary phase is often abrupt so that the decline phase is difficult to identify. Because the culture exhibits a significant cell death phase, the final cell concentration used in the calculation of (a) (iv) does not reflect the extent of culture growth supported by the substrate. The corresponding results for rS from (c) are also listed. From the From Eq. (12. 108), the observed yield of biomass from substrate YXS graph, for positive values of rX during the growth phase, the points for rX and rS fall on a straight line.Therefore, we can conclude that neither YPS.Answer: No (b) The cell concentration data produce a straight line on the semi-log plot for much of the culture period. This is an indication of exponential or first-order growth kinetics (Section 12.8.1). Answer: Yes (c) In the semi-log plot, the growth data fall on a straight line between 0 h and 50 h; the points after 50 h appear to be part of the decline and stationary phases. As the first four points appear to fall on a straight line, these may be used to evaluate the initial rate. For a system of constant volume, YPS. From Section 12.7.1, overall yields are determined using differences between the initial and final states. All of these factors mean that Z. mobilis performs better than S. cerevisiae for ethanol production. The biomass produced in ethanol fermentation by yeast is often sold for use in animal feeds, whereas application of bacteria for this purpose is not as well accepted in the industry. At constant volume, a semi-log plot of viable cell concentration versus time can also be used to evaluate kd. For each medium osmolarity, the data for viable cell concentration plotted in (a) can be fitted using a straight line for cell death during the later part of the culture period. Evaluating the observable Thiele modulus.Evaluating the observable Thiele modulus. The value of rA,obs can be determined by trial-and-error using Figure 13.14 and the equations derived above. As mass transfer is improved by reducing the thickness of the tissue, we can expect that.Results for several.Such low glucose concentrations would occur for only a very short period of time at the end of batch growth.However, if we do not know the Km value for immobilised penicillin-G amidase,.When the feed stream to the bioreactor is sterile, the observed product yield from biomass. Although maintenance is expected to have only a small effect on the answer, an alternative expression for Dopt that applies to cultures with maintenance requirements can be derived.The calculations are shown in the table below.Answer: Once every 178 days.Erfahren Sie, wie wir und unser Anzeigenpartner Google Daten sammeln und verwenden. Cookies zulassen. To browse Academia.edu and the wider internet faster and more securely, please take a few seconds to upgrade your browser. You can download the paper by clicking the button above. Stream In Out Strained Evaporated Total 33.4 133.7 501.5 191.2 859.9 33.4 133.7 501.5 191.2 859.9 All columns and rows of the completed table add up correctly. Answer: 4.7 tonnes Answer: 1.3 tonnes There are 191.2 kg of sugar in 500 kg of coulis. Answer: 38 MixturePEG stockSalt stockLeft-over 1Mixing tank. System boundary. Left-over 2ExtraThe system boundary is shown on the flow sheet. No reaction occurs. No extra data are required. No compounds are involved in reaction. As there is no reaction, the appropriate mass balance equation is Eq. (4.3): The calculation table below shows all given quantities in kg. The total mass of PEG stock in is denoted P; Stream In Out Total mass balance. PEG balance. Salt balance. Applying (2) and (3) to (1). These calculations allow completion of the mass balance table with all quantities in kg. Total 88.65 79.66 281.69 450 88.65 79.65 281.7 450 All columns and rows of the completed table add up correctly to within round-off error. From the completed mass balance table, 77.3 kg of PEG stock, 105.4 kg of salt stock, and 17.3 kg of extra Answer: 77 kg of PEG stock, 105 kg of salt stock, 17 kg of additional water Residual solutionProductSolutionSeed crystals. Fluidised-bedSystem boundaryThe system boundary is shown on the flow sheet. No reaction occurs. No extra data are required. No compounds are involved in reaction. As there is no reaction, the appropriate mass balance equation is Eq. (4. 3): The calculation table below shows all given quantities in kg. The total mass of product crystals out is Seed Product Residual Tetracycline balance. Total mass balance. Applying the result from (1): These calculations allow completion of the mass balance table with all quantities in kg. Stream In Out Seed Product Residual Total 7.704 92.3 100.004 7.704 92.30 100.004 All columns and rows of the completed table add up correctly. From the completed mass balance table, the mass of the residual solution is 94.959 kg. Answer: 95 kg From the completed mass balance table, the mass of product crystals is 5.045 kg. (We could subtract the. Answer: 5.0 kg Downstream solutionTracer solutionPipe. System boundaryThe system boundary is shown on the flow sheet. The density of 30 NaCl in water is taken to be approximately 1.2 g mlMcGraw-Hill). 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The specific requirements or preferences of your reviewing publisher, classroom teacher, institution or organization should be applied. Please enter recipient e-mail address(es). Please re-enter recipient e-mail address(es). Please enter your name. Please enter the subject. Please enter the message. Author: Pauline M DoranPlease select Ok if you would like to proceed with this request anyway. All rights reserved. You can easily create a free account. Author(s): Pauline M. Doran One is for 1st Edition. Another is for 2nd Edition and include chapter 2 to 14. Report this Document Download now Save Save Solution Manual for Bioprocess Engineering Princip. For Later 45 45 found this document useful, Mark this document as useful 55 55 found this document not useful, Mark this document as not useful Embed Share Print Download now Jump to Page You are on page 1 of 20 Search inside document Davide Cali Radiance Grace Draven Love You Forever Robert N. 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