Smog in L. Web module includes a Living Example Problem. Getting Unstuck C. Interactive Computer Games A. Quiz Show I 4. The reactor portion of this encyclopedia is included on the CRE Web site. Before solving the problems, state or sketch qualitatively the expected results or trends.
Write a paragraph describing both the content goals and the intellectual goals of the course and text. Look at the QuickTime videos. Write a paragraph describing two or more of the reactors. What similarities and differences do you observe between the reactors on the Web e. How do the used reactor prices compare with those in Table ?
Go on a scavenger hunt using the summary notes for Chapter 1 on the Web site. Take a quick look at the Web Modules and list the ones that you feel are the most novel applications of CRE. QA What does a negative number for the rate of formation of species e. What does a positive number signify?
QA What assumptions were made in the derivation of the design equation for: a The batch reactor BR? Problems PA a Revisit Example Rework this example using Equation on page Explain why. Suggest two ways to work this problem incorrectly. Play this game and then record your performance number, which indicates your mastery of the material. The feed is only A and B in equimolar proportions. Which of the following sets of equations gives the correct set of mole balances on A, B, and C?
Species A and B are disappearing and species C is being formed. Circle the correct answer where all the mole balances are correct. We shall use this system volume to model the accumulation and depletion of air pollutants. We shall perform an unsteady-state mole balance Equation 1—4 on CO as it is depleted from the basin area by a Santa Ana wind. Santa Ana winds are high-velocity winds that originate in the Mojave Desert just to the northeast of Los Angeles. Use the data in the module to work parts 1—12 a through h given in the module.
Load the Living Exam- ple Polymath code and explore the problem. These equation solvers will be used extensively in later chapters.
Also, plot the number of foxes versus the number of rabbits. Explain why the curves look the way they do. Enrico Fermi was an Italian physicist who received the Nobel Prize for his work on nuclear processes. He used a process to set bounds on the answer by saying it is probably larger than one number and smaller than another, and arrived at an answer that was within a factor of How many piano tuners are there in the city of Chicago?
Show the steps in your reasoning. How many square meters of pizza were eaten by an undergraduate student body popula- tion of 20, during the Fall term ? How many bathtubs of water will the average person drink in a lifetime?
PA What is wrong with this solution? The entering concentration of A, CA0, is 2 molar. What is the corresponding reactor volume? Rate Law 2nd order 5. For further elaboration of the development of the general balance equation, see not only the Web site www. New York: Wiley, , Chapter 4. A detailed explanation of a number of topics in this chapter can be found in the tutorials. New York: McGraw-Hill, See also Cells on questions, 26 Apparent reactions in batch reactors, — on termination, in azomethane decomposition, in cell growth, — Berzelius, J.
See Rate data collection in toluene hydrodemethylation, Creativity in reactor selection, and analysis — Cricket chirping frequency, 99 DDT dichlorodiphenyl-trichloroethane Dichlorodiphenyl-trichloroethane DDT Critiquing journal articles production, 6 production, 6 diffusion, Deactivation of catalysts Diethanolamine formation, mass transfer limitations, by coking and fouling, — Differential forms and equations Crystalline aluminosilicates, empirical decay laws, — batch reactors, 34, — Crystals in microelectronic fabrication, moving-bed reactors, — for diffusion in pellets, —, overview, — — CSTRs.
See Continuous-stirred tank by poisoning, — Ergun equation, reactors CSTRs reactors offsetting, ethylene oxide production, Cumene by sintering, — isothermal reactor design, adsorption, — straight-through transport reactors, PBRs, 19, 38, , decomposition, 5, — — PFR mole balance, 15—16 in Langmuir—Hinshelwood kinetics, temperature-time trajectories, solutions to, — — triphenyl methyl chloride-methanol rate law, — Dead volume reaction, — Cumulative distribution function, CSTRs, —, , — tubular flow reactor design equations, Curie, Marie, tubular reactors, 37 CVD chemical vapor deposition , zones, Differential reactors, rate data collection — Dean, A.
See Inhibition of ethane from, — Explosive intermediates, microreactors enzyme reactions PBRs for, — for, lock-and-key model, Ethylene chlorohydrin, Exponential cell growth, — mechanisms, — Ethylene glycol EG Exponential decay rate law in catalyst Michaelis—Menten equation, — CSTRs for, — deactivation, temperature in, from ethylene chlorohydrin and Exponential integrals, Epidemiology, PSSH for, sodium bicarbonate, External diffusion effects.
Flow rates as active intermediates, on RTD moments, mass transfer and reaction, in bimolecular reactions, 70 on tracer techniques, mass transfer correlations, Frequency factors in activation energy, Fanning friction factor, membrane reactors, , 91 Fast orange formation, — multiple reactions, Freudlich isotherms, Fed batch reactors.
See Semibatch space time, 59 Friction factor in pipe pressure drop, reactors Flow reactors, — See 79—80 Ideal gas constant, Bioreactors data for, Ideal gas law, 35 Gumbo, — external diffusion effects on. See also Temperature data for, Ignition-extinction curves, — COMSOL for, rate law parameters for, Ignition temperature CSTRs with, — Homogeneous systems, diffusion and in equilibrium conversion, in semibatch reactors, — reactions in, in multiple steady states, in steady-state nonisothermal Honeybee flight speed, Imperfect pulse injection in step tracer reactors.
See Active learning resources for, — Langmuir—Hinshelwood kinetics intermediates molar flow rates. See Bioreactors — professional reference shelf for, Microelectronic fabrication adiabatic tubular reactors, 25—26 chemical vapor deposition in, batch reactors, 10—12, — propylene glycol production, , — in design equations, 33 , — overview, — enzymatic reactions, rate data analysis, Microfluids in nonideal reactor integral data analysis, reaction rate, 4—8 modeling, — series reactions, — semibatch reactors, —, , Micromixing, , butane isomerization, , , Microorganism growth.
See Steady-state for digital-age problems, — from azomethane, — nonisothermal reactors membrane reactors for, — from benzene diazonium unsteady-state.
See Unsteady-state nonisothermal, chloride, 91 nonisothermal reactors energy balance in, — skin exposure to, Nonlinear least-squares, unsteady-state, — Nitrogen dioxide Nonlinear regression packed bed flow, from nitrogen oxide, batch reactor data analysis, — parallel.
See Plug-flow reactors PFRs in tubular reactors, — design equations for, 94 Pharmacokinetics Open systems, first law of dispersion in, competitive inhibition, — thermodynamics for, energy balance for, in drinking and driving, — Open vessel dispersion, flow reactor design equations, 37—38 modeling, — Operating conditions gas-phase reactions, summary, — mass transfer coefficients, — with heat exchange, Tarzlon, parallel reactions, — acetic anhydride production, Phases Operating costs in ethylene glycol — cell growth, production, — algorithm, — enthalpy, — Optimum feed temperature in butane isomerization, — gas.
See Gas phase and gas-phase equilibrium conversion, — mass transfer, —, — reactions Optimum yield in batch reactor series mole balances, 18—19, — heterogeneous reactions, 7 reactions, ODE solvers algorithms for, liquid. See also specific reactor types ideal reactors in diffusion, , by name batch and plug-flow, — in dispersion, , in parallel reactions, — laminar flow reactors, — Seafood gumbo, — in rate data analysis, single-CSTR, — Searching in series, 47—48 integral relationships in, — for mechanisms, — CSTRs, 48—50 internal-age distribution, — in nonlinear regression, — CSTRs and PFRs combination, mean residence time in, , Second-order ODE solutions, 53—57 measurements, — Second-order rate laws, 76 CSTRs and PFRs comparisons, moments, — Second-order reactions, 73 57—58 multiple reactions, — batch reactor data analysis, PFRs, 52 normalized function, — CSTR design, — sizing.
See Conversion and reactor PBRs, irreversible, sizing pulse input experiment for, — isothermal, —, — for toluene hydrodemethylation, step tracer experiment, — laminar flow reactors, — — T-I-S model, mean conversion, — Real reactors two-parameter models, — multiple steady states, mean conversions in, — Web site material, PBRs, — in two-parameter models, — Respiration rate of chipmunks, Second reactors in interstage cooling, Realistic models for nonideal reactors, Reversible gas-phase decompositions, — — Secondary nutrients, Reciprocal concentrations, Reversible isomerization, Segregation model Reciprocal power decay rate law, Reversible reactions, 70 in maximum mixedness model, , Recycle reactors, overview, 80—83 Recycle stream in parallel reactions, stoichiometry, — vs.
T-I-S model, in activation energy determinations, determination, zero-adjustable-parameter, — 91 in mass transfer coefficient, , , Selectivity batch reactor data analysis, — CSTRs, cell growth, in mass transfer correlations, liquid-phase reactions, , , ethylene hydrogenation to ethane, Ribonucleic acid RNA , membrane reactors for, , — — Robert the Worrier, — multiple reactions, —, , methane production, — RTDs.
See also specific adiabatic operation. See Energy balances deactivation, , instructions, equilibrium conversion. See Flow Separation systems, economic incentive Solar energy reactors for, biochar gasification, information required for, — Sequencing of reactors, 57—58 chemical storage, questions and problems, — Series, reactors in, 47—48 field design, summary, — combinations, 53—57 water splitting, — supplementary reading, — CSTRs, 48—50 Solid catalysts in PBRs, 18 Steady-state operation in chemostats, design, —, — Solvents from ethylene oxide, PFRs, 52 Space satellite maneuvering, — Step tracer experiment, — Series reactions, Space time, 58—60 Stern—Volmer equation, — batch reactors, — in CSTR modeling, Stirred reactors blood clotting, — in dispersion coefficient CSTRs.
See Steady-state straight-through transport reactors, CVD, — nonisothermal reactors microelectronic fabrication, unsteady-state. See Mass transfers Ultrasonic waves, light from, — Vat reactors. Vermont SERI , light from, — series reactions in batch reactors, Vessel boundary conditions splitting, — dispersion coefficient determination, Water-gas shift reaction, equilibrium — constant in, — Z tubular reactors, — Watson, K.
Chemic By Karine Veiga. P e Example See Polymath program Pe. Part 1 Calculated values of the DEQ variables Variable initial value minimal value maximal value final value t 0 0 24 24 Cc 2. Consequently, the concentration of product is very low compared to the case without uncompetitive inhibition.
Part 3 Change the observed reaction rate constant: 0. Thus CP the plots for this part are approximately the same as the plots in part 1. And at low temperature PSSH results show greatest disparity. Eventually everyone is ill and people start dying. This explains the shape of the figure. Case2: With drug inhibition Reactions: 1.
Thus the stoichiometry equation will be changed. This is not realistic as at some point there will be too many cells to fit into a finite sized reactor. Either a cell death rate must be included or the cells cannot be recycled. PROD max 1 0. Then, Rate of decrease of conc.
Now, since the concentration is very less assuming there is no constraint of sunlight. Since the number of days is coming less than 4. Hence, the initial assumption is verified. P The following errors are present in this solution- 1. It should be S for Hanes-Woolf form. The expression for intercept is correct but the slope is given wrong.
The correct expressions are - 5. As concentration of inhibitor I increases, slope increases. In the given plot, slope for line 1 is more as compared to line 2 in spite of having lower concentrations. This implies that the concentration values are switched. Also the numerically calculated slope values are wrong. At 40 atm, we had While, at 80 atm we have This is not possible and the model should be discarded. Model f is the worst model of all. Assume H2 in the gas phase reacts with C2H6 adsorbed on the surface and ethane goes directly into the gas phase.
P c Individualized solution. S expression, the constant should be KA2 instead of KDC 2 The overall site balance should include the product, as it too is getting adsorbed. S rC kc CC. Therefore, the inlet temperature we would recommend is K. P d Aspen Problem P e 1 2 At high To, the graph becomes asymptotic to the X-axis, that is the conversion approaches 0. At low To, the conversion approaches 1.
P f. P d The only change to the Polymath code from part b is that the heat of reaction changes sign. The new code is not shown, but the plots are below. This means heat is generated during the reaction and there is no advantage to adding inerts as there was in the endothermic case. See Polymath program Pe. Now weed need expressions for CB and CC. Variable Value 1 T The entering temperature for reactor 1 is now K and the outlet is K.
This means that the slope of the conversion line from the energy balance is larger for reactor 2 than reactor 1. So the line for conversion in reactor 3 will be steeper than that of reactor 2. The mass balance equations are the same as in part b and so the plot of equilibrium conversion will decrease from reactor 1 to reactor 2, and, likewise, from reactor 2 to reactor 3.
Hence the heat exchanger needs to be changed in order that the heat removed by the exchanger is such that the maximum temperature in the reactor does not go above K at any point during the operation. Variation of entering feed temperature: i Keeping other conditions constant we change value of T0 only now. The plot of Qg and Qr with V is as shown; Similarly other unsafe operating conditions can be found out keeping in view that the heat generated during the course of the reaction, is not removed efficiently by the exchanger such that there is a wide difference between the two terms at any position in the reactor.
See polymath program P The rate of reaction for all cases is decreasing because the temperature of the system is decreasing with volume. The rate of reaction for counter-current heat exchanger system is a U shaped curve plotted against volume. At the front of the reactor, the reaction takes place very rapidly, drawing energy from the sensible heat of the gas causing the gas temperature to drop because the heat exchanger cannot supply energy at an equal or greater rate.
This drop in temperature, coupled with the consumption of reactants, slows the reaction rate as we move down the reactor. See polymath code Pb 6. In the case of adiabatic operation this phenomenon is very significant. In case of constant heat exchange fluid temperature the effect of inert gas is negligible. The Ta value will be changed and the program will be tested for following values of Ta.
T will be greater i CPC 35 Vary 0. Thus we see that if we go on increasing the value of residence time, firstly the number of steady states will increase and then it will start decreasing. By trial and error, an inert flow rate of 6. That is, the residence time is short, so the exit conversion is small. At small Fao, the residence time is long, so the exit conversion is large. Notice that at low Fao, the conversion reaches equilibrium conversion, while at high Fao, the conversion does not reach equilibrium conversion.
Low concentration of A slower reaction rate lower conversion and less heat evolved by the reaction that is, lower temperature in the reactor. Thus, at high Ua the reactor temperature is low. The lower reactor temperature causes reaction rate to be slow, and thus lower conversion is observed. He has been research advisor to forty-five Ph. Pruitt Award from the Council for Chemical Research. Method of Excess Scott Fogler. To promote the transfer of key skills to real-life settings, Fogler presents three styles of problems: Straightforward problems that reinforce the principles of chemical reaction engineering Living Example Problems LEPs that allow students to rapidly explore the issues and look for optimal solutions Open-ended problems that encourage students to use inquiry-based learning to practice creative problem-solving skills About the Web Site umich.
Show and hide more. Table of contents Product information. Mole Balances 1. Conversion and Reactor Sizing 2. Rate Laws 3. Stoichiometry 4. Isothermal Reactor Design: Conversion 5. View larger. Preview this title online. Request a copy. Download instructor resources. Additional order info. Buy this product. K educators : This link is for individuals purchasing with credit cards or PayPal only. Scott Fogler builds on the strengths of the previous edition to enable students to learn chemical reaction engineering through logic rather than memorization.
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