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document | lilU \;"AI"U:.R;) HererogeoeOIJS \ ;atalYSIS
It must be emphasized that step 2 is not an elementary step, but a sum of all of the
quasi-equilibrated steps that must occur after dinitrogen adsorption. According to this
abbreviated sequence, the only species on the surface of the catalyst of any kinetic rel
evance is N*... | null | {
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document | at the emphasis on chemical reaction engineering as opposed
to chemical reactor engineering is the appropriate context for training future chemi
cal engineers who will confront issues in diverse sectors of employment.
We gratefully acknowledge Prof. Michel Boudart who encouraged us to write this
text and who has provi... | null | {
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document | 200 CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions
used to determine the observed rate of reaction in the presence of diffusional
limitations.
(6.3.36)
(6.3.37)3robs
TJ=-=
f max
Substituting Equations (6.3.35) and (6.3.36) into (6.3.34) gives:
o dCA I47T(Rp)-D'TA~ r=R
p
4 3
"37T (Rp )... | null | {
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document | 4 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
The next task in describing a chemically reacting system is the identifica
tion of the reactions and their arrangement in a network. The kinetic analysis of
the network is then necessary for obtaining information on the rates of individ
ual... | null | {
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document | CHAPTER 8 Nonideal Flow in Beacto,.wrs~ --,,2..6.......1
li(i',) = 0
li(O) = 2u
~ -
:
\
I
V
\ V
\ I I
,,~ v V
L-.. i -
Parabolic velocity
distribution li(i')
Figure 8.1.1 I Schematic representation of laminar
velocity profile in a circular tube.
uAc dCA----
Ac dz
dCAu-
dz
Integration of this equation with CA = C~ at t... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_0967aacb3e9e57f4 | 1,788,540,066.175081 | 1.0 |
document | Diffusivity
effective, 196
transition, 191
typical values, 186
Dihydrogen, See also Hydrogen
in ammonia synthesis, 1-3, 159-160,250-251
associative desorption of, 153
chemisorption, on platinum, 138-139
dibromine, reaction with, 131-132
dichlorine, reaction with, 101
as inhibitor, 171, 250-251
olefin hydrogenation, efl... | null | {
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document | 172 CHAPTER 5 HeterogeneQlls Catalysis
approximation together with any other assumptions, like a rate-determining step, a
most abundant reaction intermediate, etc. and compared to the rate data. If the func
tional dependence of the data is similar to the proposed rate expression, then the se
quence of elementary step... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_5c84e0140391d4b4 | 1,788,540,066.153023 | 1.0 |
document | e distribution data for, 284-285
semibatch reactors as, 67
Fertilizers, 2
Fick's First Law
axial dispersion model and, 273
cylindrical pores, ideal, 193
derivation of, 350, 352
external transport effects and, 186
Finlayson, B. A., 323
First order reactions
rate expressions for, 24, 26 (table), 26-29
residence time dist... | null | {
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document | __~_7
Microkinetic Analysis
of Catalytic Reactions
7.1 I Introduction
A catalytic reaction consists of many elementary steps that comprise an overall
mechanistic path of a chemical transformation. Although rigorous reaction mecha
nisms are known for simple chemical reactions, many catalytic reactions have been
adequat... | null | {
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document | _________ ------'A""""--J~ B
Regression Analysis
B.1 I Method of Least Squares
Below is illustrated the method of least squares to fit a straight line to a set of
data points (Yh x;). Extensions to nonlinear least squares fits are discussed in
Section BA.
Consider the problem of fitting a set of data (Y" x;) where y an... | null | {
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document | 30 C HA PT E R 1 The Basics Qf Reaction Kinetics for Chemical ReactiQn Engineering
From Equations (1.3.4) and (1.5.8):
1 dni
r=
vY dt
or
(variable V)
(constant V)
dnAV- = -knAnBdt
dCA
- = -kCAC B
dt
dPA k
dt = - R r PAPB [constant V: Ci = pJ(R~T)]
g
(1.5.9)
(1.5.10)
(1.5.11)
For second-order kinetic processes, the limi... | null | {
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document | ___________ -'C>LI:IHLliAuP~T.......EnRL7L~~l'f.lyliJtic..cDRJ;;1eC.'acvJtlJ..iollJn"'"s_~ ~2...5'.L7
Although many kinetic models assume that the catalyst is an ideal Langmuir sur
face (all sites have identical thermodynamic properties and there are no interactions
among surface species), modern surface science has p... | null | {
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document | VIGNETTE 8.4.11
CHAPTER 8 Nonldeal Flow in Reactors 277
B. G. Anderson et aL [Ind. Chern. Res.. 37 (1998) 815] obtained in situ of
pulses of IlC-Iabeled alkanes that were passing through packed beds of zeolites us-
ing positron emission tomography (PET). PET is a technique developed primarily for
nuclear medicine that ... | null | {
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document | CHAPTER 3 Reactors for Meas!!ring Reaction Rates 99
takes place in a constant volume batch reactor that has a safety disk designed
to rupture when the pressure exceeds 1000 psi. If the rate constant is 0.01 s-1,
how long will it take to rupture the safety disk if pure A is charged into the
reactor at 500 psi?
14. If yo... | null | {
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document | 174 CHAPTER 5 Heterogeneous Catalysis
[A] in feed
Figure 5.4.1 I
Results from Case I where adsorption is
the rate-determining step.
[A] in feed
Figure 5.4.2 I
Results from Cases 2 and 3 where surface
reaction or product desorption is the rate
determining step.
step, then extra B in the feed effectively competes for su... | null | {
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document | e observed reaction orders be explained
if adsorbed ethylene (*C2H4 *) were the most abundant reaction intennediate?
Explain your answer.
6. Read the paper entitled "Microkinetics Modeling of the Hydroisomerization of
n-Hexane," by A. van de Runstraat, J. van Grondelle, and R. A. van Santen,
Ind. Eng. Chem. Res., 36 (1... | null | {
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document | r to
provide a greater stabilization against thermal runaway?
• Answer
Since this example comes from the simulation of a real reactor, the amount of data neces
sary to completely describe it is very high. Thus, only the trends observed will be illustrated
in order to conserve the length of presentation.
Schematically,... | null | {
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document | 256 CHAPTER 7 Microkinetic Analysis of Catalytic Reactions
that the overall heat of reaction for step 3 is about 3 kJ mol- J endothermic on a Pd
surface. In principle, these types of calculations can be performed on all of the
species in the Horiuti-Polanyi mechanism, and the results can be used in a subse
quent kinet... | null | {
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document | CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions
Sc =
pDAS
up(2R p )
Re = ----'------'---
t-t
189
(6.2.23)
(6.2.24)
where t-t is the viscosity (kg m-] s-]), p is the fluid density (kg m-3), and u is the
linear fluid velocity (m s-]). However, most mass-transfer results are correlated in... | null | {
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document | ustrial conditions of high pressure. The last example involving
ethylene hydrogenation revealed how quantum chemical calculations provide esti
mates of the energies associated with elementary steps on catalytic surfaces that can
be subsequently used in reaction simulations. Finally, microkinetic analysis is clearly
mo... | null | {
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document | CHAPTER 5 HeterogeneolJs Catalysis 149
that of the surface reaction step. The surface reaction is thus called the rate
determining step (RDS) since nearly all of the free energy change for the overall
reaction is associated with that step. In general, if a rate determining step exists,
all other steps in the catalytic... | null | {
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document | CHAPTER 7 Microkinetic Analysis of Catalytic Reactions 259
example of a reaction involving a bifunctional catalyst, where a transition metal
component facilitates hydrogenation/dehydrogenation and an acidic component
catalyzes structural rearrangement. Section 5.3 illustrates the important
reactions involved in hydroca... | null | {
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document | 356 Index
Barner, H, K, 235
Barnett, L. G" 237
Bateh reactors
adiabatic operation, 291-293
analogy to PFRs, 77
defined, 64, 65-67
laboratory scale, 84-87
material balance for, 65, 83 (table)
nonisothelmal operation, 288-294
reactor conversion predietion assumptions and, 269
variables for, vs. flow reactors, 74 (table)
... | null | {
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document | CHAPTER 1 The-.BBS.icsof Reaction Kinetics fOLChemical Reaction Engineering
k(~) (1 - JA)[M - JA]
(1 + SAJA)
EXAMPLE 1.5.4 I
31
(1.5.16)
Equal volumes of 0.2 M trimethylamine and 0.2 M n-propylbromine (both in benzene)
were mixed, sealed in glass tubes, and placed into a constant temperature bath at 412 K.
After variou... | null | {
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document | 362 Index
Large scale reactions--C Ol1t.
commercial reactor, 328 (photograph)
ethylene oxide production, 93-94
fructose, from enzyme catalysis, 117
hydroformylations, 36-37, 68, 69 (figure)
maleic anhydride production, 333
transport phenomena and rates of, 184-185
Lauryl alcohol, 37
Law of Definitive Proportions
define... | null | {
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document | 328 CHAPTER 10 Reactors Accomplishing Heterogen.CLeo'-"leuls:LL1Rs;;;.eacuc'"'t.LI.ioan""s _
10.4 I Reactor Configurations
Thus far, fixed-bed reactor descriptions have been presented. Schematic represen
tations of fixed-bed reactors are provided in Figure 10.4.1, and a photograph of a
commercial reactor is provided i... | null | {
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document | 126 CHAPTER 4 The Steady-State Appmximatioo' Catalysis
kinetic parameters for this system. This method is typically called "isotopic tran
sient kinetic analysis."
Figure 4.3.la shows a schematic of an apparatus to perform the steady-state,
isotopic transient kinetic analysis for the hydrogenolysis of ethane over a Ru/... | null | {
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document | ks, 44-45
parallel networks, 43
series reaction networks, 41
Young, L. C., 323
z
Zeolite catalysts
axial-dispersion coefficients, 277
for catalytic cracking, 331-332
described, 164 (figure), 165 (figure), 166-170
in ethylbenzene alkylation, 235-236
Zero intercept, in linear regression, 32, 345-347,
346 (table)
Zewail, ... | null | {
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document | Data:
VAil 9000 J/(min-K)
T~. 323 K (and is constant)
v 100 L/min
c2 O. 10 mol/L
All other data are from Example 9.5. I .
• Answer
The material balance equation remains the same as in Example 9.5.1. The energy balance is
now:
VAIl (T~ - T) 6.HrF~j~ + F~ (I - fA)Cp, (T TO) + F~ (3 2j~)CpfJ (T - TO)
+ 2F~fA CfJc (T - TO)... | null | {
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document | "'2...8"'O'-- -"C....H1Aou:P"-'TuE --- _
gives the same result as a material balance on the system (see Example
3.4.3).
4. Calculate the mean concentration of A at the outlet (z L) of a laminar flow,
tubular reactor (C ~) accomplishing a second-order reaction (kC 1), and
compare the result to that obtained from a PFR w... | null | {
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document | McGraw-Hill Higher Education 'ZZ
A Division of The MGraw-Hill Companies
FUNDAMENTALS OF CHEMICAL REACTION ENGINEERING
Published by McGraw-Hili, a business unit of The McGraw-Hili Companies, Inc., 1221 Avenue of the
Americas, New York, NY 10020. Copyright © 2003 by The McGraw-Hili Companies, Inc. All rights reserved.
No... | null | {
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document | CHAPTER 4 The Steady-State Approximation Catalysis 129
S. Enzymes are more commonly involved in the reaction of two substrates to
form products. In this problem, analyze the specific case of the "ping pong bi
bi" mechanism [w. W. Cleland, Biochim. Biophys. Acta, 67 (1963) 104] for
the irreversible enzymatic conversion ... | null | {
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document | CHAPTER 9 Nooisothermal Reactors 313
Calculate the volume and heat removed from the CSTR and the PFR. Do the
magnitudes of the heat being removed appear feasible? Why or why not?
Data:
C = 45 cal mol- l K- 1
PA
C = 40 cal mol- 1 K- 1
Pp
- liHr 10,000 cal mol- l
C~ = 1.5 mol L- 1
F~ = 100 mol min- l
9. The ester of an o... | null | {
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document | APPENDIX B Regression Analysis 347
Reduction and Error Analysis for the Physical Sciences, McGraw-Hill, New York,
1969, p. 114):
~2 == N _1 2 '" (y,. ~ ~ X)2v .:::;.; '-<] - '-<2 i (B.3.3)
for the linear equation (B.1.1). (The sample variance is the sum of squares of the
residuals divided by the number of data points m... | null | {
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document | t composition [pathway (III)].
That is,
I
T,;,,,,
= !::..H . - .. + MS IC dTQ r ITinitial (fmal Illitlal) final \ Pfinaj)
Tinitial
(9.3.5)
where a positive value for the heat of reaction denotes an endothermic reaction.
Since the reaction-rate expressions normally employ moles of species in their
evaluation:
I
T,;"",
M... | null | {
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document | E, 250, 251
Rowland, M., 265
R,R-l ,2-bis[(phenyl-o-anisol)phosphino ]ethane (DIPAMP),
241-245 | null | {
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document | CHAPTER 5 Heterogeneolls I;StSIYSIS l"1l
The total number of adsorption sites on the surface now appears explicitly in the
rate expression for this elementary adsorption step. Since the site balance is the same
as before (Equation 5.2.5), the equilibrium adsorption isotherm can be calculated in
the manner described abo... | null | {
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document | 60 CHAPTER 2 Rate Constants of Elementary Reactions
If Equation (2.3.9) is compared to Equation (2.2.1), then:
A= (~) exp [ A:gt ]
E= AHt
(2.3.10)
(2.3.11)
The data of McKenzie et al. clearly show that as the energy barrier increases (higher
E), the entropy of activation becomes more positive (larger ASt implies more
f... | null | {
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document | CHAPTER 5 Heterogeoeolls Catalysis 173
This particular sequence assumes both A* and B* are present on the surface in ki
netically significant amounts. The rate expression for this case is:
r = rz = kz[A*]
[A*]K =--
I [A ][*]
[B*]K =--
3 [B][*]
[*]0 = [*] + [A*] + [B*]
kz[*Jo[A]r = ------=--"---'---
1 + KI[A] + K3 [B]
... | null | {
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document | imit as Ar approaches zero yields the following differential equation:
(6.3.23)
The flux of A can be expressed in terms of concentration for binary systems ac
cording to Fick's Law (in spherical coordinates):
(equimolar counterdiffusion) (6.3.24) | null | {
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document | x Contents
7.3 Ammonia Synthesis on Transition Metal
Catalysts 246
7.4 Ethylene Hydrogenation on Transition
Metals 252
7.5 Concluding Remarks 257
Chapter 8
Nonideal Flow in Reactors 260
8.1 Introduction 260
8.2 Residence Time Distribution (RTD) 262
8.3 Application of RTD Functions to the
Prediction of Reactor Conversio... | null | {
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document | rogeneous Catalysis, American Chem
ical Society, Washington, D.C., 1993, p. 145).
In the case of ammonia synthesis on transition metal catalysts, a variety of
reasonable paths with various levels of complexity can be proposed. For the sake
of clarity, only one such path will be presented here. Stolze and Norskov suc
... | null | {
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document | __~~6
Effects of Transport
Limitations on Rates
of Solid-Catalyzed
Reactions
6.1 I Introduction
To most effectively utilize a catalyst in a commercial operation, the reaction rate
is often adjusted to be approximately the same order of magnitude as the rates
of transport phenomena. If a catalyst particle in an industri... | null | {
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document | 314 CHAPTER 9 Nonisotbermal Reactors
The following data are known:
k1 = 103 exp(-2500/T)s-l, TinK
AHr = -lOkcalmol- 1
K = 8 at 300 K
Cp = 1 kcal kg- 1 K- 1
P = 1 kg L- 1
(a) For a reactor space time of 10 min, what is the conversion for a 300 K
operating temperature? What is the conversion at 500 K? (Remember: the
equi... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_5d29350c24ef7bcb | 1,788,540,066.186088 | 1.0 |
document | 26 CHAPTER 1 The Basics of Reaction KinAtics for Chemical Reaction Engineering
Table 1.5.1 I Examples of reactions that can be described using first-order reaction
rates.
Isomerizations
Decompositions
Radioactive decay
(each decay can be described
by a first-order reaction rate)
N20 S ===> N02 + N03
CH2 CH2 ===> CH4 + ... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_781fd091794d1023 | 1,788,540,066.124079 | 1.0 |
document | 146 CHAPTER 5 Heterogeneous Catalysis
Isolated A cannot desorb as A2
Isolated vacan
site cannot
dissociate A2
A A A 1 1 A
A A A A A A
t A A A A
- A A A A A
A A if ~ A A A
A A A A A A A A
A A A
A A A A A A
A A A A A
A A A A A A
A A A A
A A
Figure 5.2.5 I
Schematic depiction of a square lattice populated by A
atoms. Empt... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_269527debcb188f0 | 1,788,540,066.144026 | 1.0 |
document | 246 CHAPTER 7 MicrQkinetic Analysis Qf Catalytic ReactiQns
inverse relationship between intermediate and product selectivity and the unusual
effect of dihydrogen pressure on product selectivity observed during asymmetric
hydrogenation of prochiral olefins with a chiral catalyst.
7.3 I Ammonia Synthesis on
Transition Me... | null | {
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document | 140 CHAPTER 5 Heterogeneolls Catalysis
5.2 I Kinetics of Elementary Steps:
Adsorption, Desorption, and
Surface Reaction
The necessary first step in a heterogeneous catalytic reaction involves activation of a
reactant molecule by adsorption onto a catalyst surface. The activation step implies
that a fairly strong chemic... | null | {
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document | 254 CHAPTER 7 Microkinetic Analysis of Catalytic Reactions
of dihydrogen pressure and a 100 K span in temperature. The observed order of
reaction with respect to dihydrogen increases from 0.47 at 223 K to 1.10 at 336 K.
Clearly, the kinetic model reproduces the observed rates at all of the conditions
tested. The model ... | null | {
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document | 162
EXAMPLE 5.3.2 I
CHAPTER 5 Heterogeneolls Catalysis
of the mario All other steps have no kinetic significance. In fact, they may be
reversible, in part or in whole.
3. All equilibrated steps following a rate-determining step that produces the
mari may be summed up in an overall equilibrium reaction. Similarly, all
e... | null | {
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document | 70 CHAPTER 3 Beartors Inc MeaslJfjng Boaction Batos
The volume in the reactor is changing due to the input of methanol in benzene. Thus, the
volume in the reactor at any time is:
V 3.78(100 + t)
Therefore,
0.204 - 0.263 n~nsl[3.78(100 +
where
From Equation (1.2.6),
dna
dt -0.263 fI~flB/[3.78(100 + t)F
n~ = O@ t 0
ng = ... | null | {
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document | -Hexene
hydration of, 292-293
hydroformylation of, 85
isomerization of, 202-203
Hicks, J. S., 216
Hill, C. G., Jr., 54, 66, 78, 235, 299, 334
Hinrichsen, 0., 250, 251
Holies, J. H., 181
Homogeneous vs. heterogeneous catalysis, 133,
315-317
Horiuti, J., 252, 253, 256
Hot spots, 303, 309-310
Hudson, J. L, 96, 233
Hurwitz... | null | {
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document | CHAPTER 8 Nonideal Flow in Reactors
1
1
----:
1 I
Fi~ :~Fi+dFi
----1_-1-----
1 I
1 dz I
I I
273
"'AXiallY-diSpersed
~PFR
de
Fi = uACCi - ACDadf
Figure 8.4.1 I
Descriptions for the molar flow rate of species i in a
PFR and an axially-dispersed PFR. Ac : cross-sectional
diameter of tube, u: linear velocity, Da : axial di... | null | {
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document | eries)
Includes index.
ISBN 0-07-245007-X (acid-free paper) - ISBN 0-07-119260-3 (acid-free paper: ISE)
I. Chemical processes. I. Davis, Robert J. II. Title. III. Series.
TP155.7 .D38 2003
660'.28-dc21 [REDACTED_PHONE]
CIP
INTERNATIONAL EDITION ISBN 0-07-119260-3
Copyright © 2003. Exclusive rights by The McGraw-Hill Co... | null | {
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},
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document | CHAPTER 5 Heterogeneolls Catalysis
Concentrationof A
Figure 5.2.4 I
Langmuir Adsorption Isothenn: Fractional coverage 8A
versus fluid phase concentration of A.
145
When more than one type of molecule can adsorb on the catalyst surface, the
competition for unoccupied sites must be considered. For the adsorption of molec... | null | {
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document | C H A PT E R 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions 187
(6.2.7)
Since the flux of A must be constant through the stagnant film (conservation of
mass), the derivative of the flux with respect to distance in the film must vanish:
dNA, =0dx
Differentiating Equation (6.2.6) (assuming cons... | null | {
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document | , ....
EXAMPLE 5.2.2 I
I.inAr I en:l nH1Hrouefje01JS \ i8IalYSlS
are believed to occur through Rideal-Eley steps. Apparently, the conditions typical of
semiconductor growth favor Rideal-Eley elementary steps whereas conditions normally
encountered with catalytic reactions favor Langmuir-Hinshelwood steps. This point is... | null | {
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document | rphase, 220
nonisothermal reactions, 212-217
spherical catalyst pellets, 199-202
Effluent streams, dyes in, 48-49
Elementary steps
adsorption, in heterogeneous catalysis, 140-147
Arrhenius' Law and, 54-56
defined, 4
desorption, in heterogeneous catalysis, 155-156
microkinetic analysis and, 240, 248
notation for, xvi (t... | null | {
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document | 42 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
Consider the reaction network of two irreversible (one-way), first-order reac
tions in parallel:
yDP
A
~SP (1.5.33)
Again, like the series network shown in Equation (1.5.22), the parallel network of
Equation (1.5.33) can represent a variety... | null | {
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document | dence of the rate is also affected by diffusional limitations. Since the ob
served rate constant, kobs, is proportional to (D~Ak)2, the observed activation energy is
(ED E)/2, where ED is the activation energy for diffusion and E is the activation en
ergy for reaction. Diffusional processes are weakly activated compa... | null | {
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document | 19a
EXAMPLE 5.2.1 I
cnAPTl!fJ:t HeTerogeneous L8T81YSIS
Use the steady-state approximation to derive the rate expression given in Equation (5.2.22).
kads
(1) A + * ( ) A* (reversible adsorption)kdes
k,
(2) A* ---"-+ products + * (surface reaction)
• Answer
The rate of the reaction is:
A ===;> products
r = k2 [A*]
(over... | null | {
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document | 8 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
Chemical Bond: Structure and Dynamics, Academic Press, 1992). However, in
the vast majority of cases, chemically reacting systems are investigated in much
less detail. The level of sophistication that is conducted is normally dictated by
the ... | null | {
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document | CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions
0.8
vo 0.6
s1cJ 0.4
0.2
0
0 0.2 0.4 0.6 0.8
Figure 6.3.7 I
Effect of Thiele modulus on the nonnalized concentration
profiles in a spherical catalyst particle with first-order
reaction. The external surface of the particle is located at
r/... | null | {
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document | 222 CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions
with boundary conditions:
d'IJI-=0
dX
d'IJI
dX = Bim (1 - 'IJI)
at X = 0
at X = 1
(6.4.20)
(6.4.21)
As discussed previously, the general solution of the differential equation is:
(6.4.22)
The constants are evaluated by using the appro... | null | {
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document | 66 CHAPTER 3 Reactors for MeaslJring Reaction Rates
v(t)
Batch Semibatch
EXAMPLE 3.2.1 I
Figure 3.2.1 I
Ideal batch and semibatch reactors. vet) is a volumetric
flow rate that can vary with time.
An important class of carbon-carbon bond coupling reactions is the Diels-Alder reactions.
An example of a Diels-Alder reacti... | null | {
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document | CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions 215
(6.3.91)
(6.3.92)
(6.3.94)
r=~Ts
The rate constant k(T) is expressed in terms of Ts by first forming the ratio:
:&!J ~ exp [ - : G-;J] ~ exp[ -'(f-I)] (6.3.93)
where:
Ey=
RgTs
The dimensionless group y is known as the Arrhenius numbe... | null | {
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document | 238 CHAPTER 6 Effects of Transport I imitations on Rates of Solid Catalyzed Reactions
Consider the effect of the Biot number significant if it changes 1]0 by more
than I percent. Can you draw any qualitative conclusions from the behavior
observed in parts (a)-(d)?
15. The liquid-phase hydrogenation of cyclohexene to cy... | null | {
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document | CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering 9
EXAMPLE 1.2.1 I
If there are several simultaneous reactions taking place, generalize Equation (1.2.1) to a sys
tem of NRXN different reactions. For the methane oxidation network shown in Scheme 1.1.1,
write out the relationships from the gen... | null | {
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document | APPENDIX C Transport in PorOllS Media 351
Now consider a multicomponent system. For a multicomponent mixture of
NCOMP species:
(Cl.8)
by analogy to the frictional force for a binary mixture [Equation (C.l.l) with Equa
tion (CIA)]. Using Equation (C.l.8) gives a total force balance of:
-dX. NCOMP XX(V - V)
1 = 2: 1) 1 ... | null | {
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document | 96 CHAPTER 3 Reactors for Measilring Reaction Rates
(b) What is CX in a PFR with recycle shown below?
5 Lmin- 1
10 Lmin- 1
c;]= 1.2molL-l ce
A
(c) Now, add a separator to the system. Find C1, c1, C~ and c1. For the sepa
rator, assume cX = 5CX.
5 Lmin- 1
10 Lmin- 1
C~=1.2molL-l
Separator . ce
A
(Problem provided by Pro... | null | {
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document | CHAPTER 5 Heterogeneolls Catalysis
Table 5.1.1 I Determination of metal particle size on Pt/AI2 0 3 catalysts by
chemisorption of H2 and CO, X-ray diffraction, and transmission
electron microscopy.
139
0.6a 1.2 1.3 1.3
2.0a 1.6 1.8 2.2
3.7" 2.7 2.9 2.7
3.7b 3.9 4.6
1.6
1.8
2.4
5.3
VIGNETTE 5.1.2
apretreatment temperatu... | null | {
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document | s the value of 4Ujdt that is necessary to bring the outlet
temperature to approximately the value given in Example 1O.2.1?
2. Plot the dimensionless concentration and temperature profiles for the reactor
system given in Example 10.2.2 for Pea = BOa = 00 and compare them to those
obtained when Pea = BOa = 15.
3. Reprodu... | null | {
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document | 98 CHAPTER 3 Reactors for Measllring Reaction Rates
11. Titanium dioxide particles are used to brighten paints. They are produced by
gas-phase oxidation of TiCl4 vapor in a hydrocarbon flame. The dominant
reaction is hydrolysis,
The reaction rate is first-order in TiC14 and zero-order in H2 0. The rate con
stant for t... | null | {
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document | d mix
ing. The pulse will appear at a time t1 = to + T, where T is the space time (T = Vjv).
However, with the CSTR, the pulse emerges as an exponential decay in tracer con
centration, since there is an exponential distribution in residence times [see Equation
(3.3.11)]. For all nonideal reactors, the results must li... | null | {
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document | 67 (figure)
Transient material balance expressions
axial-dispersion model, 272-274
radial-dispersion model, 282
Transition diffusivity, 191
Transition state intermediates
defined, 5, 6, 7 (figure)
ethyicne hydrogenation, 254 (figure)
Transition state theory, 56-62
vs. Arrhenius form, 60
genera] equation of, 58-59
poten... | null | {
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document | CHAPTER 5 HeterogeneolJs l;atalYSIS
5.3 I Kinetics of Overall Reactions
Hit
Consider the entire sequence of elementary steps comprising a surface-catalyzed reac
tion: adsorption ofreactant(s), surface reaction(s), and finally desorption ofproduct(s).
If the surface is considered uniform (i.e., all surface sites are id... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_4bcf40e14d7dbad0 | 1,788,540,066.149034 | 1.0 |
document | C H A PT E R 9 NonisolhermaLR""e""'8c"'1"-'ow:ts'-- --"3....0LL1
or
U(T* (9.4.6)
U(T* - T)i = '" FC dT _ !:.H,IToFO die
d ~ I Pi dV Vo e dVt I R , R
(9.4.7)
Using the fact that:
Equation (9.4.7) can be written as:
dT
'" FC =-7' I Pi dVR
* 4!:.H,ITo)r - U(T - T )-dt
(9.4.8)
Thus, the material and energy balances for the... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_d36b3b40f51f99b4 | 1,788,540,066.182088 | 1.0 |
document | 336 CHAPTER 10 Reactors Accomplishing Heterogeneolls Reactions
k1exp[-k2RT]P&P~r
r] = -1-+-k-P-k6-+-k-P-k8---'~'---k-P-k-1O 1bmoI/(lbeat-h)
S 0, 7 DT 9 VA
kl1 exp[ -k12RT]P&JP0A
k k" k lbmoI/(lbcat-h)
1 + ksPo~ + k7P DT + kgP..j'A
where PT is the total pressure and:
k] = 1.771 X 10- 3
k2 = 23295.0
k3 = 0.5
k4 = 1.0
ks ... | null | {
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document | 20 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
infonnation can often be derived for rates of individual steps, and reactors can be
designed for carrying out the reaction at optimum conditions.
Below are listed general rules on the fonn of the reaction rate function (M.
Boudart, Kinetics ... | null | {
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document | 76 C HAP T E R 3 Reactors tQLMeascUlILU'inJjg,J--UR.CLe=ac"'-'t,,-iQ,,-"nJRJ s,,--~~~~~~~~~~~~
where
v = '1/1 + V E 2.36 Llh
C~ C/lVH/v 0.00289mol/L
(-u/I)r = kC/lC E
Since the outlet value of CH is known, the fractionalconversionand CE can be calculatedas:
and
0.00289 - 0.001094
0.00289
0.62
Thus,
C~
CEVE
-- - C~fH = ... | null | {
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document | • Answer
The material balance for the batch reactor is:
d'j'
~=kCO(I-t·)·(1.2 j"dt A . A A)
The energy balance can be written as:
'(' )_A (Jdj~lJAH T - T - I..>. H, nA di +
The material and energy balance equations must be solved simultaneously. A convenient form
for solution by numerical techniques is:
dfA
dt
dT
dt n~... | null | {
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document | 38 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
°excess air II excess air
CH3CH20H > CH3C- H > 2C02 + 2H20
ethanol acetaldehyde
For this situation the desired product is typically B, and the difficulty arises in how
to obtain the maximum concentration of B given a particular kj and k2 • U... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_9c0765e8fa56c71b | 1,788,540,066.126078 | 1.0 |
document | um particles
supported on MgO [0. Hinrichsen, F. Rosowski, M. Muhler, and G. Ertl, Chern.
Eng. Sci., 51 (1996) 1683]. In contrast to the model in Table 7.3.1, the dissocia
tive adsorption of dinitrogen is represented by a single step. Many of the rate con
stants in Table 7.3.2 were determined from independent steady-... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_f535a1eea279ada0 | 1,788,540,066.17108 | 1.0 |
document | 312 CHAPTER 9 Nonisothermal Reactors
3. Plot the fractional conversion and temperature as a function of time for the
batch reactor system described in Example 9.3.3 if the reactor is now adiabatic
(U = 0). Compare your results to those for the nonisothermal situation given
in Figure 9.3.3. How much energy is removed fr... | null | {
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"char_count": 1486
} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_f9d98b17f709dadb | 1,788,540,066.185088 | 1.0 |
document | _______Jl2J>LN~JX A Revjnw of CJocBmicaLEqlJi'ibria
(A.1.l4)
and
(A.l.l 5)
Since LlCo is not a function of pressure, it is clear that pressure has no influence on Ka .
A.2 I Determination of Equilibrium
Compositions
Consider a gas-phase reaction. If the Lewis and Randall mixing rules are used
(simplest form of mixing r... | null | {
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document | Fundamentals of Chemical
Reaction Engineering
Fundal11entals of Chel11ical
Reaction Engineering
Mark E. Davis
California Institute of Technology
Robert J. Davis
University of Virginia
Boston Burr Ridge, IL Dubuque, IA Madison, WI New York San Francisco St. Louis
Bangkok Bogota Caracas Kuala Lumpur Lisbon London Madrid... | null | {
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document | 262 CHAPTER 8 Nonideal Flow in Reactors
(ICACr)u(r)2r.rdr
·0
u(r)2r.rdr
Thus, the mean outlet concentration of A, C~, can be obtained by evaluating CA at z L. For
(kL)/u I the outlet value of CA from the PFR, C~, is 0.368 C~ while for the laminar-flow re
actor C~ 0.443 C~. Thus, the deviation from PFR behavior can be ... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_e1525687e95ad939 | 1,788,540,066.175081 | 1.0 |
document | T
his book is an introduction to the quantitative treatment of chemical reaction en
gineering. The level of the presentation is what we consider appropriate for a
one-semester course. The text provides a balanced approach to the understanding
of: (1) both homogeneous and heterogeneous reacting systems and (2) both che... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_f774749124344557 | 1,788,540,066.11608 | 1.0 |
document | 212 C H A PT E B 6 Effects of Transport I Imitations on Bates of Solid-Catalyzed Reactions
From the stoichiometry of the hydrogenation reaction, the ratios of the fluxes of the compo
nents are:
3 and
Substitution of these relations into Equation (6.3.66) gives the appropriate flux equations:
(6.3.70)
(6.3.71)
Finally,... | null | {
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document | lHDEX _
A
Absorption of beer, modeling of 97
Aeetaldehyde ~ ,
decomposition of, 126
formation of, 178-179
Acetic acid, formation of, 78-79
Aeetone
formation of, 47-48, 63, 179, 231
rate function properties, 20 (figure)
Acetylene, vinyl chloride from, 47
N-Acetyl-phenylalanine methyl ester,
formation of, 241-246
Acid ca... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_98b5893a94ced588 | 1,788,540,066.195246 | 1.0 |
document | C HAP T E RiO Reactor~8cCDmplishinQ-He1erngBlliillU5Beactions 317
that occurs within the catalyst particle to the rate that would occur at the local, bulk
fluid conditions.
To maximize the reaction rate in the fixed-bed reactor, 710 should be equal to
one. In order to do this, smaller particles are necessary (see Chapt... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_85e73b4e2c094b9a | 1,788,540,066.187081 | 1.0 |
document | 258 CHAPTER 7 Microkinetic Analysis of Catalytic Reactions
Kinetic parameters for the asymmetric hydrogenation of MAC catalyzed by
Rh(R,R-DIPAMP).
k l (L mmo!-I 5- 1)
k- I (5- 1)
k2 (L mmo!-I 5- 1)
4.9
13.3
10.7
2.32 X 104
8.53 X 108
7.04 X 104
6.9
13.0
7.5
1.21 X 106
9.94 X 109
1.84 X 105
a Activation energy, kcal mol... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_8a544cac0d848ee1 | 1,788,540,066.173082 | 1.0 |
document | the feed suggests that the second case is the preferred
path.
It is possible to generalize the treatment of single-path reactions when a most
abundant reaction intermediate (mari) can be assumed. According to M. Boudart
and G. Djega-Mariadassou (Kinetics of Heterogeneous Catalytic Reactions, Prince
ton University Pres... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_9036e863635cd93f | 1,788,540,066.150029 | 1.0 |
document | 202 CHAPTER 6 Effects of Transport I imitations on Rates of Solid-Catalyzed Reactions
0.1
0.1 1
0
10
Figure 6.3.9 I
Effectiveness factor [T/ = tanh(4>0)/4>0] for a first-order
reaction in a catalyst as a function of the Thiele modulus
with generalized length parameter.
According to the above definitions, the effective... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_8537f03d2fbaab64 | 1,788,540,066.161023 | 1.0 |
document | 308
EXAMPLE 9.6.1 I
CHAPTER 9 Nonisothermal Reactors
Calculate the steady-states for the following reactor configuration. Is there an unstable steady-state?
Data:
A + B =} 2C in the liquid phase, V = I L, k 33 X 109 exp [-20,000/(R gDJ L/(mol . min),
- tJ.Hr = 20 kcal/mol, C~ 20 mol/L, C~ = 3 mol/L, v = 100 cm3/min, TO... | null | {
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document | as the nitrating agent as illustrated below:
NOz
N,o, +2 U=2 O+H'O
(A) (8) (e) (D)
If this reaction is conducted in an adiabatic CSTR, what is the reactor volume and space time
necessary to achieve 35 percent conversion of NzOs? The reaction rate is first order in A and
second order inB.
Data:
I::.Hr = -370.1 kllmol
Cp... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_77fc7ce34a1954bc | 1,788,540,066.183048 | 1.0 |
document | of, 150-151,237
fonnation of, 18-19,210-212,230,238-239
Cyclohexene
fonnation of, 299-300
hydrogenation of, 18-19,230,238-239
Cyclopentadiene, 66-67
Cylindrical catalyst pellets
diffusion/reaction in, 203-206
Index
infinite, 196-197,201 (table)
thennal conductivity effect, 218-219
Cylindrical pores, diffusion through,... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_2aeaafd4435391f3 | 1,788,540,066.197295 | 1.0 |
document | CHAPTER 9 Nooisothermal Reactors 291
and recalling the definition of the extent of reaction in terms of the fractional
conversion [Equation (1.2.10)] gives:
(9.3.8)
or in differential form:
-6.H r l ro dIe:L . dTUAH(T* - T) = n~- + (nC)-vee dt j I P, dt
Notice that [see Equations (1.2.10) and (1.3.2)]:
(9.3.9)
n~ dIe
-... | null | {
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} | C:\Users\rober\DataForge\raw_data\(McGraw-Hill chemical engineering series) Mark E. E. Davis, Robert J. J. Davis - Fundamentals of Chemical Reaction Engineering-McGraw-Hill (2003).pdf | document_4295cd5cf062b5cc | 1,788,540,066.181084 | 1.0 |
document | 22 CHAPTER 1 The Basics of Reaction Kinetics for Chemical Reaction Engineering
80 70
T (OC)
60 50 40
10
8
6
4
~
2
.S
9
N
E- 1.0"0
E- 0.8
'"0 0.6x
"'"
0.4
0.2
0.1
2.8 2.9 3.0 3.1
lX10 3 (Kr l
T
3.2
Figure 1.4.2 I
A typical Arrhenius plot, In k vs liT. The slope
corresponds to -EIRg- Adapted from D. E. Mears and M.
Bouda... | null | {
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