Chemical Reaction EngineeringHouston In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 Chemical Reaction EngineeringHouston Vern W Weekman, Jr., EDITOR Mobil Research and Development Company Dan Luss, EDITOR University of Houston The Fifth International Symposium on Chemical Reaction Engineering co-sponsored by the American Chemical Society, the American Institute of Chemical Engineers, the Canadian Society for Chemical Engineering, and the European Federation of Chemical Engineering, held at the Hyatt Regency Hotel, Houston, T X , March 13-15, 1978 65 ACS SYMPOSIUM SERIES AMERICAN CHEMICAL SOCIETY WASHINGTON, D.C 1978 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 Library of Congress CIP Data International Symposium on Chemical Reaction Engineering, 5th, Houston, Tex., 1978 Chemical reaction engineering—Houston (ACS symposium series; 65 ISSN 0097-6156) Bibliography: p Includes index Chemical engineering—Congresses Chemical reactions—Congresses I Weekman, Vern W II Luss, Dan, 1938III American Chemical Society IV American Chemical Society ACS symposiu TP5.I67 1978 ISBN 0-8412-0401-2 660.2'9'9 77-25340 ACSMC 65 1-619 (1978) Copyright © 1978 American Chemical Society All Rights Reserved T h e appearance of the code at the bottom of the first page of each article in this volume indicates the copyright owner's consent that reprographic copies of the article may be made for personal or internal use or for the personal or internal use of specific clients T h i s consent is given o n the condition, however, that the copier pay the stated per copy fee through the Copyright Clearance Center, Inc for copying beyond that permitted by Sections 107 or 108 of the U S Copyright Law T h i s consent does not extend to copying or transmission by any means—graphic or electronic—for any other purpose, such as for general distribution, for advertising or promotional purposes, for creating new collective works, for resale, or for information storage and retrieval systems T h e citation of trade names and/or names of manufacturers i n this publication is not to be construed as an endorsement or as approval by ACS of the commercial products or services referenced herein; nor should the mere reference herein to any drawing, specification, chemical process, or other data be regarded as a license or as a conveyance of any right or permission, to the holder, reader, or any other person or corporation, to manufacture, repro­ duce, use, or sell any patented invention or copyrighted work that may i n any way be related thereto PRINTED IN THE UNITED STATES OF AMERICA In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 ACS Symposium Series Robert F Gould, Editor Advisory Board Kenneth B Bischoff Donald G Crosby Jeremiah P Freeman E Desmond Goddard Jack Halpern Robert A Hofstader James P Lodge John L Margrave Nina I McClelland John B Pfeiffer Joseph V Rodricks F Sherwood Rowland Alan C Sartorelli Raymond B Seymour Roy L Whistler Aaron Wold In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 FOREWORD The ACS SYMPOSIU a medium for publishing symposia quickly in book form The format of the SERIES parallels that of the continuing ADVANCES IN CHEMISTRY SERIES except that in order to save time the papers are not typeset but are reproduced as they are submitted by the authors in camera-ready form As a further means of saving time, the papers are not edited or reviewed except by the symposium chairman, who becomes editor of the book Papers published in the ACS SYMPOSIUM SERIES are original contributions not published elsewhere in whole or major part and include reports of research as well as reviews since symposia may embrace both types of presentation In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 PREFACE has, as in past symposia, provided an excellent forum for reviewing recent accomplishments in theory and application This international symposium series grew out of the earlier European Symposia on Chemical Reaction Engineering which began in 1957 In 1966, as part of the American Chemical Society Industrial and Engineering Chemistry Division's Summer Symposium series, a meeting was devoted to chemical reaction engineering and kinetics This meeting highlighted the great interest and activity in this field in the United States, and led the organizers to join with the America European Federation of Chemical Engineers in organizing International Symposia on Chemical Reaction Engineering The first symposium was held in Washington in 1970 and was followed by symposia in Amsterdam (1972), Chicago (1974), and Heidelberg (1976) These meetings consistently attract experts in the field who have submitted many more papers than can be accommodated This year was no exception with more than 130 papers being submitted, only 48 of which could be accepted Again, the international flavor was maintained with more than one-half the papers coming from Western Europe, in addition to one each from Russia, Japan, Australia, and Canada While industrial participation was not as extensive as anticipated (30% ), it did show clearly the increasing and productive application of Reaction Engineering tools to industrial problems The meeting format maintained three plenary review lectures each morning and three parallel, original paper sessions in the afternoon The nine plenary review papers are being published in the American Chemical Society Symposium Series as a separate volume We acknowledge financial support from the National Science Foundation, American Chemical Society-Petroleum Research Fund, Shell Oil Co., Mobil Oil Corp., and Exxon Co A V E R N W W E E K M A N , JR D A N Luss Mobile Research Corp Princeton, NJ University of Houston Houston, T X October 1977 xi In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 Organizing Committee for the Fifth International Symposium on Chemica Vern W Weekman, Jr., Editor Dan Luss, Editor Members: Chandler H Barkelew (Shell Development Co.) K B Bischoff (University of Delaware) John B Butt (Northwestern University) James M Douglas (University of Massachusetts) Hugh M Hulburt (Northwestern University) Donald N Miller (Dupont Co.) xii In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 Design and Operation of a Novel Impinging Jet Infrared Cell-Recycle Reactor R LEUTE and I G DALLA LANA Department of Chemical Engineering, University of Alberta, Edmonton, Alberta, Canada In the study of chemisorbed species on catalyst surfaces, the application of infrared spectroscopic methods has developed from the early in situ studies of Eischens and Pliskin [1] to rather detailed surface kinetics measurements [5] The variety of techniques which have been described [1,2,3,4,5,6,7,8] increase i n their effectiveness with their a b i l i t y to discriminate between the spectra of adsorbed species which are relevant to the reaction mechanism and spectra of spurious adsorbed species These approaches may be c l a s s i f i e d using this c r i t e r i o n as follows: (i) I n t r i n s i c Rates/Surface Spectra Transients Measured D i r e c t l y Under reaction conditions where adsorbed reactants, intermediates, and products display significant IR absorption band i n t e n s i t i e s , the transient intensities may be quantita­ t i v e l y monitored Considerable detailed studies are required to correlate these intensities with surface concen­ trations (ii) Global Rates/Surface Spectra Static or Transient By carrying out studies i n an IR cell - c i r c u l a t i o n flow reactor, a cause-and-effect r e l a t i o n between reactant concentration and specific band intensities may be discerned Such mechanistic insights may be useful i n developing more r e l i a b l e forms of rate expressions (iii) Indirect Studies of Adsorption and Surface Reactions The observation of selected spectral band intensities attributed to chemisorbed species are assumed to be related to the surface reactions involved I f the spectra are recorded at room temperature, the presence of spurious spectra may occur Generally, additional experimental evidence is required to demonstrate the relevance of such observations to the kinetics of the c a t a l y t i c reaction © 0-8412-0401-2/78/47-065-003$05.00/0 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 CHEMICAL REACTION ENGINEERING—HOUSTON This paper d e s c r i b e s the development of an improved v e r s i o n of the IR cell-recycle r e a c t o r (type ( i i ) ) which is to be used to study the mechanism and kinetics of r e a c t i o n s of 2-propanol on v a r i o u s alumina c a t a l y s t s While t h i s r e a c t i o n does not have direct commercial i m p l i c a t i o n s (dehydration or dehydrogenation), it e x h i b i t s many of the characteristics which make it very s u i t a b l e to demonstrate the usefulness of the IR technique Design Factors The yin AAXU technique i n v o l v e s c a t a l y s t p e l l e t s i n the form of very t h i n wafers, about 40 mg/cm2 alumina content The h i g h s u r f a c e area, about m^/cm^- of IR beam c r o s s - s e c t i o n , enables s u f f i c i e n t adsorbed species to i n t e r a c t w i t h the IR beam even a t r e l a t i v e l y low s u r f a c e coverage that s p e c t r a w i t h good I n s t u d y i n g s o l i d - c a t a l y z e d gas-phase r e a c t i o n s , the back­ ground s p e c t r a r e s u l t i n g from the gas-phase are u s u a l l y e l i m i n a t e d by use of a double-beam IR spectrophotometer, i n which the sample c e l l i s matched w i t h an " i d e n t i c a l " reference c e l l without c a t a l y s t i n i t V a r i a t i o n s i n pressure and/or temperature between sample and reference c e l l s i n c r e a s e the d i f f i c u l t y of matching the two c e l l s When the c a t a l y s t wafer i s placed t r a n s v e r s e t o the flow of gases through the IR c e l l - r e a c t o r , the flow p a t t e r n s w i t h i n the c e l l l e a d to c o n c e n t r a t i o n gradients along the a x i s of the IR beam, and between the f r o n t and r e a r s u r f a c e concentrations on the wafer Under r e a c t i o n c o n d i t i o n s , these aspects l i m i t the s e n s i t i v i t y of the technique because of low s u r f a c e coverages a t r e a c t i o n temperatures The new c e l l attempts t o e l i m i n a t e many of these o b j e c t i o n a b l e f e a t u r e s Figure l a describes a t y p i c a l geometry f o r previous c e l l designs I t should be evident that i t i s d i f f i c u l t to o b t a i n values of the i n t r i n s i c r e a c t i o n r a t e because of the uneven c o n t a c t i n g between the gas and wafer a t v a r i o u s p o i n t s on the wafer s u r f a c e High r e c i r c u l a t i o n r a t e s w i t h i n such a steadys t a t e r e c y c l e r e a c t o r provide d i f f e r e n t i a l values of the r e a c t i o n r a t e , but these g l o b a l values are u n l i k e l y to equal i n t r i n s i c r a t e s ( n e g l e c t i n g , f o r the moment, i n t r a p a r t i c l e d i f f u s i o n ) C o m p a t i b i l i t y of flow p a t t e r n s between the IR c e l l and an i d e a l continuous s t i r r e d - t a n k r e a c t o r are r e q u i r e d as a minimum c o n d i t i o n Since the mode of h e a t i n g the wafer l i k e l y i n v o l v e s IR-transparent windows being a t temperatures lower than those of the wafer, compensation f o r temperature gradients may a l s o be required Figure l b describes the proposed geometry of the improved IR c e l l - r e a c t o r This r e c y c l e r e a c t o r i s t o be capable of being operated i n e i t h e r open (flow) o r c l o s e d (batch) modes of o p e r a t i o n The r e a c t o r u n i t i s maintained a t the r e a c t i o n temper­ ature (up t o 400°C) and the pump and sampling system are maintained at a constant u s u a l l y lower temperature (220°C) t o ensure maximum In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 605 INDEX Equation ( s ) ( continued ) intrinsic rate mass balance mass transport Michaelis-Menten Monod of motion, Navier-Stokes for oxidation of ethylene pressure drop radical reaction reaction rate with the Schmidt number steady-state continuity Stokes-Einstein for trickle-bed reactors, performance tubeside reactor Wilsons Equilibrator, external hydrogen Equilibrium constant Equilibrium flash Equipment, experimental Escape probability for a particle 416 430 73 164 164 72, 73 80 271 350 414 76 492 73 331 389 21 35 428 585 430 238 572 Experiments, results of loop reactor 21 Exponential model 297 Expression, Corrsin 130 Expression, Lennard-Jones 77 Extinction temperature 98,101 F Factorial design, orthogonal Factorial design for reactor gas composition Fan, flywheel/ Feed concentration, hydrogen makeup apparatus effluent analysis equipment, cyclic mixture, argon 586 585 51 531 529 482 teristics or 431 Feedstocks 255 Fermentation 153,154 Fermentors air-lift 154-157 comparison of various 160 Escherichia coli 164 loop 154,159,160 Ethane 535 mechanically stirred 154-156 conversion of 544 performances of various 153 cracking furnace 271 Fick's law 64 gas inlet temperature, measured 439 conversion of 546 "Fines" content 247 Ethane yields 531 Finite bed boundary condition Ethyl acetate 574 Finite perturbations, transient behavior of the reactor for 568 Ethylbenzene 315-322 273 decomposition 320,321 Fire box heat transfer 26, 63 molar concentrations of 323 Fischer-Tropsch synthesis pyrolysis of 313-316 Fixed-bed adiabatic methanator 70 Ethylbenzyl 316 catalytic reactor 513 disintegration of the 318 catalytic reformer 283 Ethylene 207,316-322 kinetic data 59 concentration 531 reactor(s) 539 profile 535 cell model studies of radial flow 550 ethane, vapor phase catalytic trickling 447 hydrogénation of acetylene 526 reforming pilot plant, isothermal 287 hydrogénation of 512 155 molar concentrations of 323 Flat-blade turbine 220 oxidation of 77,80,440 Flexibility consideration in the design of styrene, molar concentrations of 321 multitubular reactors 214 Evaluation of the plugging time, analytical 228 Flow ammonia yields for centripetal Exchanger radial 550 heat 353 axial 554-557 monolithic reactor-heat 83, 89 behavior, fluid 571 systems, simple heat 215 cocurrent 216 Exit profile 144 control operation 562 Expansion, gas 438 countercurrent 216,363 Experimental methods 190 diagram, process 454 Experimental study of velocity and fixed bed reactors, cell model concentration profiles 72 studies of radial 550 Experiments, L P A 317 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 606 CHEMICAL REACTION ENGINEERING—HOUSTON Flow (continued) increases with gas velocity and "fines" content, interstitial 439 laminar 72 methods, heat 37 model, diffusion/convection 577 modes, M R H E 87 modes of operation, open in packed beds, axial 541 patterns in typical ir-cell reactors plug 72 polymerization of E P D M polymer, laminar 140 radial 553,554 inlet 541 rate of coolant 220 rate, heat 38 reactor(s) catalyst utilization in a trickl for hydrotreating heavy oil, trickle 425 isothermal continuous 526 plug 428 trickle 431 recycle 584 steady state temperature profiles, axial 552 velocity profile analytic solution for nonuniform viscous 149 Fluid(s) field 216 flow behavior 571 interstitial velocity 551 mixing behavior 571 Newtonian 73, 74 nonNewtonian 149 Fluid dynamic parameters in bubble column design, determination of 372 Fluid dynamic properties 362 Fluidized-bed reactor 563 model(s) 436,438 modeling the slugging 400 Fluxes, heat 273, 277 Force balance on transport cell 419 Formation of C 488 Formation rate, straight chain paraffins 33 Foulant deposit geometries 201, 202 Fouling from interactions of pore structure and foulant deposit geometries 201 Fourier law 190 Frankel, Dufort and, methods 67 Frequency factors, rate equation parameters 22 spectral stability diagram with curves of equal 502 G Gas (es) 63,310 analysis system 513 bubble 401 in a bubbling fluidized bed 436 chromatograph 315,513 flame ionization type 528 method 531 composition, Arrhenius plot of reaction rate with 587 composition, orthogonal factorial design for reactor 585 dense-phase 401 exchange 401,402 rate 441 expansion 438, 440 flow rate, molar 360 inlet temperature, measured conversion of ethane 546 linear velocity 375-380 -liquid chromatograph 207 interface 428 mass transfer 387 coefficients 311 reactor(s) 351-353 systems 373 tube reactor, cocurrent 329 phase absorbance sample cells 12 absorption, double-beam compensation for 10 concentration 366 dispersion coefficient 379,381 equilibrated 583 intrapellet 463 mole fraction of C 367 profile 365 reactions 4, 447 development of reaction models for complex 313 temperature variations 479 profiles 368,369 -solid mixing 51 noncatalytic reactions 226 reactions, pore plugging model for 225 systems 554 solubilities 593 temperature, inlet gas 544 velocity and "fines" content 439 Gears algorithm 103 Geometries, nature of the interaction of the pore structure and foulant deposit 201,202 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 INDEX 607 Glass tubular reactor 207 Global rates Glucose concentration 165-171 Glucose consumption rate 170 Graetz problem 89 Grain models 225 Grain size, variation of 225 Grignard-reagent, formation 44, 45 Growth in batch and continuous culture 168 kinetical analysis of unbalanced bacterial 163 rate 163 reciprocal plots between the specific 167 specific 165,169 at varying temperatures, specific Gulf-patented segmented bed reactor 166 transfer (continued) property, temperature dependence of radiative Henry's law 362, Heptanes Heterogeneous catalysis, adsorption in Heuristic approach to complex kinetics Hexanes Hinschelwood equation, Langmuir— Hinschelwood, kinetic models, Langmuir— Homogeneous continuum heat transfer models 47 273 588 288 50 292 288 209 57 239 Homopolymerization Hougen and Watson kinetic models Hovmand and Davidson, model of 408, 409 32,34 Hatta numbers 125 Hydrocarbon(s) chlorination of saturated 440 Hazards, assessment of thermal 43, 45 distribution, steady state, and Heat periodic effluent 529 of adsorption 57 thermal decomposition reactions of 313 types of reaction 63 trace 479 balances in matrix notation 273 306 capacities 41 Hydrocracking reactions 307 diffusivity, flow control operation Hydrodesulfurization 254-261,387 of a plug-flow tubular reactor of residual oils 255 with high 562 of thiophene 207 evolution, rate of 41 exchanger 353 Hydrodynamic entrance effect 89 monolithic reactor— 83, 89 Hydrofluorination of U 440 run Hydrogen 288,307, 448 cocurrent reactor93 cycling, feed 533 countercurrent reactor92 donor reactions 306 for the pellet-filled reactor90 equilibrator, external 428 systems, simple 215 feed concentration 531 flow mole fractions of 517, 532 calorimeters 37-40 peroxide, nitric acid, catalytic control principles 38 decomposition of 505 methods 37 reduction of ores 440 rate 38 styrene, molar concentrations of 321 flux (es) 277 -styrene ratio 319 methods, linear 190 sulfide 448 nonradiative 273 uptake, desulfurization and 433 profile 271 Hydrogénation of reaction 41 of acetylene, ethylene, ethane, transfer vapor phase catalytic 526 coefficient 45, 89, 241, 249,498 of butadiene 515 control, method of 38 of 2-butanone 411,414 data 247 carbon monoxide 26 fire box 273 of ethylene 512 mechanism 218, 250 of α-methylstyrene 414 models, homogeneous continuum 239 on nickel catalysts, dynamic in packed beds of low studies of acetylene 526 tube/particle diameter ratio 238 solvent 311 parameters 15 in trickle-bed reactor, butanone 413 H In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 CHEMICAL REACTION ENGINEERING—HOUSTON 608 Hydrolyse, isothermal run of acetic anhydride 42 Hydrotreating heavy oil, trickle flow reactors for 425 Hyperbolic model 295-298 Hysteresis 53,101 in the conversion-inlet temperature domain 467 curves 99-101,477 in wall-catalyzed reactors 98 I I B M model, equivalence between the SA model and the 133 Ideal mixing ( C S T R ) 14 Ignition point apparatus ( Ή Ρ Α ) , therma temperatures 98,10 zone 101 Industrial reactors, performance of 571 Infinite bed boundary condition 241 Information System, (TIS) Technological 352 Infrared beam, reference cell cell-reactors 3-5,10 spectrometer spectrophotometer 4-6 Initiator limitations 175 Instrumentation, thermal 37 Integral reactor 15,17, 462 advantages of 22 carbon monoxide oxidation in an 461 concentration 21 experiments 20 temperature distribution 21 Integration constant determination 66 routine, Rung-Kutta variable step size 103 rule, Simpson's 286 Intensity function 576-580 representation of residence time variability 571 Interface axial distribution of fractional active sites at fluid-solid 115 gas/liquid 428 liquid/solid 428 spectrophotometer-computer Interstitial flow increases with gas velocity and "fines" content 439 Iodine concentration against D a number 128 Iodine consumption 126 Ionization chamber, electron impact 314 Ionization type gas chromatograph, flame 528 Iron 191 Isobutene 359 Isomerization, of P ( O C H ) 44 Isoperibolic calorimetry, aceumullation method 37 Isotherm, Langmuir 464, 465 Isothermal conditions 388 continuous flow reactor 526 fixed-bed reforming pilot plant 287 heterogeneous fixed-bed catalytic reactor 512 multiplicities 461 reactor 72 reforming reactor profiles 289 run 42-44 Isotropic transport 420 3 J Jet stirring Jones expression, Lennard- 136 77 Κ Ketone aqueous solution 412 methyl ethyl 574 vapor pressure 421 Kieselguhr catalyst 513 Kinetic(s) 41 activity 282 effect of catalyst pretreatment on 35 Arrhenius 563 parameters 318 of catalytic liquefaction of Big Horn coal 303 data 586 fixed-bed 59 desulfurization 447 determination of the realtime activity 287 design data from a bench-scale heatflow calorimeter 37 form ( C P A F ) , copolymer approximate 182 heuristic approach to complex 292 of the liquid diffusion regime 590 measurements 3,15, 26 modeling for oscillatory catalytic reactions 487 models 57-59,453,488-490 nonlinear 301 parameters 22 penultimate effect 175 phi-factor 175 reforming model 282 resistance 225,230 selectivity 282 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 609 INDEX Kinetic(s) (continued) studies with a spinning basket reactor, multiphase S oxidation Kummer's hyper geometric function Kutta variable step size integration routine, Runge2 447 582 113 103 L L91 L I N S E I S equipment 191 L P A experiments 317 LP91 L I N S E I S conductometer 192 Lag dynamic 41 influence of time 566 temperature 57 time 568 Laminar flow polymerization of E P D M polymer 140 Langmuir -Hinschelwood adsorption mechanism 283 equation 209 kinetic models 57 isotherm 464, 465 monolayer theory 516 LaPlace-transformation 340 Late reaction zone phenomenon, early559 Law of Arrhenius 500 Law, Fick's 64 Law, Fourier 190 Law, Henry's 362,588 Law, Michaelis-Menten 126 Layer diffusion, product 226 Least square, nonlinear 309 Legendre polynomials 542 Lennard-Jones expression 77 Limestone, absorption of S by calcined 225 Limestone, comparison with experimental data for sulfation of fully calcined 231 Limit cycle(s) 506 experimental 493 frequency of 500 phenomena during catalytic oxidation reactions over a supported platinum catalyst 475 simulated 493 Limtiation region, diffusion 77, 80 Linear heat flux methods 190 regression methods 295 statistical methods 292 velocity, gas 375-380 Liquefaction of Big Horn coal, kinetics of catalytic 303 process (es) 303-306 Liquid diffusion influence 582 regime, kinetics of the 590 resistance 592 distribution in a trickle-bed 417 full upflow reactor 428 -gas chromatograph 207 -gas systems 373 interface, gas/ 428 - l i q u i d spray column 539 - l i q u i d systems 373 phase deviation from plug flow 387 dispersion coefficient 379,380 mass transfer coefficient 367 geneous 388 -solid interface 428 -solid transport 393 velocity dependence of reaction rates 415-418 Loop fermentors 154-160 Loop reactor 15-18 advantages of 22-25 data with pilot plant experiments, comparison of 24 design of 17 experiments, results of 21 M Macromixing 126 Macromolecular content 163—165 Magnetic deflection mass spectrometer 477 Maleic anhydride from benzene, production of 215 Maleic anhydride, oxidation of benzene to 440 Manganese-containing catalysts 26 Mass balance 64-66 equation 430 spectrometer, magnetic deflection 477 spectrometer, time of flight 314 transfer 8,153,154 in absorption without reaction 329 in a bubble column, C0 -interphase 359 with chemical reaction, regime of 327 coefficient 8,9,365-367 effects 306 factors 57 interphase 428 limitations 428 parameters 15 performance rates 13 representation of reactants 418 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 610 CHEMICAL REACTION ENGINEERING—HOUSTON transfer (continued) on selectivity, influence of 327, 328 in stirred cell reactor during sulfonation 329 in a trickle-bed reactor, mathe­ matical model of 420 transport to the catalyst bed, con­ centration changes caused by 68 transport equation 73 Material balances 405,406 Matrix eigenvalues of the selectivity 284 eigenvectors of the selectivity 284 notation 283 heat balances in 273 selectivity rate constant 285 truncation on catalyst effectiveness effect of 39 Measurement(s) heat flow 38 kinetic 1,15,26 transient rapid response 50 Mechanical stirring, relative efficiency of 134 Mechanically stirred fermentors 154-156 Mechanism(s) heat transfer 218, 250 of interaction 125 reaction 488 Mechanistic model 404, 408,409 Melt 585 Menten's equation, Michaelis126,164 Metal catalyst, oxidation of carbon monoxide over 83 deposition on the desulfurization activity, effect of 262 removal in a stirred-tank reactor 260 sulfide deposits 258 Methanation 63,70 Methane 316 Method(s) ASTM 193 collocation 542 dynamic 195,196 experimental 190 linear heat flux 190 regression 295 statistical 292 perturbation 564 collocation 232-235 Rung-Kutta 315 static 190,195 steady state 339 thermal 37 Thomas 143 two-plate 191 unsteady state 339 water displacement 513 Methyl ethyl ketone 574 Methylstyrene, hydrogénation of α- 414 Michaelis-Menten's equation 125,126,164 Micro-methods 38 Micromixing effects 126 experimental parameters for 127 phenomena in continuous stirred reactors 125 time(s) 129-131,134 Mid-Continent naphtha 287, 288 Middle East residues 255,261, 262 Mini-pilot reactor 37 Minimum lifetime 259-262 Mixed flow profiles 220 Mixed flow reactor 219 axial 304,337-345 behavior, fluid 571 gas-solid 51 radial 304-306 (STR), ideal 14 Model(s) axial dispersion 242, 307, 359 axially dispersed plug flow 239 for complex gas-phase reactions, development of reaction 313 countercurrent backmixing 400 diffusion/convection flow 577 dual site 455 evaluation of 243 exponential 297 fluidized bed reactor 436, 438 for gas-solid reactions, pore plugging 225 homogeneous continuum heat transfer 239 Hougen and Watson kinetic 57 of Hovmand and Davidson 408, 409 hyperbolic 295-298 kinetic 59,453,488, 490 Langmuir—Hinschelwood kinetic 57 of the liquid distribution in a trickle-bed 417 of mass transfers in a trickle-bed reactor 42C mechanistic 403, 404, 408, 40S Monod's 17C nonlinear kinetic 301 one-dimensional dispersion 372 "parallel bundle" 202 plug flow 242-244 pore plugging 226,231, 233, 23S pore structure 20c for prediction of the radial conductivities 241 pseudomonomolecular kinetic reforming 282 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 INDEX 611 Monad's (continued) for reaction in partly wetted catalyst pellets 391 "shrinking aggregate" 130 slugging fluidized bed reactor 400 621 spectrophotometer studies of radial flow, fixed bed reactors, cell 550 time-averaged 408, 409 trickle-bed reactor 411 two-phase 400-403,539 dispersion 359 "wedge layering" 202 Modeling for oscillatory catalytic reactions, kinetic 487 Modulus, Thiele 34, 99,125 Moisture-free coal 307 Molar concentrations 321-32 Molar gas flow rate 360 Mole fraction 515 of C , gas phase 367 feed hydrogen 532 of H 517 profiles for different thermal conductivities 102 Molecular conductivity 248 Molten V - K S catalyst, oxida­ tion of S on supported 582 Monod's equation 164 Monod's model 170 Monolith(s) channels 72,103 entrance effect in active 80 catalysts, poisoning in 110 convertor, concentration, and velocity profiles 72 pellet-filled 83-85 physical dimensions of crossflow 84 reactor (active wall) 72 reactor-heat exchanger 83, 89 Monomer disappearance 143 Monomer sensitivity limitations 175 Monte Carlo integrations 275 Movement, cocurrent-countercurrent 539 Moving bed reactor, design of a 540 Multi-component adsorption, effects of 51, 57 Multiphase kinetic studies with a spinning basket reactor 447-449 Multiplicity 551 during C O oxidation, steady state 477 measured and calculated, ranges of 547 phenomena 499 steady state 98 and uniqueness, regions of 545 upper and lower temperature profiles region or 546 in wall-catalyzed reactors 98 Multitubular reactor(s) 215 Mutta technique, Runge90 2 2 Ν Naphtha 306 Arab light 287,288 Mid-Continent 287,288 Nigerian 287 Naphthalene sublimation rate of Navier-Stokes equation of motion 72,73 Nelder and Mead, derivative-free simplex method 22 Newton-Raphson algorithm 88 iteration 114 method 103 procedure 273 Newtonian fluid 73,74 catalysis, dynamic studies of acetylene hydrogénation on 526 content 531 Nigerian naphtha 287 Nitric acid, catalytic decomposition of hydrogen peroxide 505 Nitric oxide conversion 550 Nitrogen 425 Noncatalytic homogeneous liquid phase reaction 388 Noncatalytic reactions, gas-solid 226 Nonisothermal behavior in chain addition copolymerization 173 Nonisothermal histories 180 Nonlinear kinetic models 301 Nonlinear least square 309 Non-Newtonian fluids 149 Nonradiative heat fluxes 273 Nonselective poisoning 110-111,115 cell 555,556 fractional yield as function of cell 558 Nusselt 99 Peclet 248, 249,308, 338-344,578-580 Prandtl 248 Reynolds 243-249, 465 wall biot 249, 251 Nylon-6 348 Nyquist plane 566-569 Oil(s) dibenzothiophene in white flush furnace heavy fuel trickle flow reactors for hydrotreating heavy vaporized white One-dimensional dispersion model In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 310 447 307 306 306 425 448 448 372 CHEMICAL REACTION ENGINEERING—HOUSTON 612 Packed bed ( s ) ( continued ) Operating time on catalyst perform­ axial flow in 541 ance, effect of 29 of low tube/particle diameter Operation on the selectivity of ratio, heat transfer in 238 catalytic reactions, effect of periodic 512 Packed bubble columns of large diameter, axial mixing of Ores, hydrogen reduction of 440 liquid in 337 Organism and growth medium 163 Packing efficiency 346 Orthogonal central-composite 345 design 293 Packing on axial mixing, effect of 339,344 Orthogonal collocation 67,103 Pall rings 288 Orthogonal design 584-586 Paraffin composition profiles Paraffin formation rate, straight chain 33 Oscillation ( s ) 202 amplitude of temperature 503 "Parallel bundle" model Parallel passage reactor asymmetric behavior of the advantage of 70 temperature 503 dimensions of 65 of concentration 568 methanation in a 63 at different temperatures 480-483 experimental period in compariso with computed period 50 Parallel reaction mechanism 309 from computer simulation, typical temperature 501 Parameter(s) cross-correlations 247 in a stirred tank reactor, theoretical and experimental study of heat transfer 15 mass transfer 15 self-sustained 498 of a pseudomonomolecular kinetic of temperature and conversion 508,568 reforming model, realtime Oscillatory catalytic reactions, activity 282 kinetic modeling for 487 RA 175 Oscillatory phenomena 482 search technique, Rosenbrock's 287 Oxidation 99,173 of anol to anone 348 Parametric sensitivity 30 of benzene 217, 440 Partial pressure of carbon monoxide of butane 574 Particle(s) catalyst 417 1-butene 482 diameter ratio, heat transfer in carbon monoxide 83,465,466,476,491 packed beds of low tube/ 238 cyclohexane 354, 356 diffusional resistance through the of dammitol 292, 294 pores of the 225 efficiency 352 escape probability for a 572 of ethylene 77,80, 440 size 584 in an integral reactor, carbon monoxide 461 Particulate phase, piston-flow region of 405 kinetics, S 582 Peclet Pe number 242,248,249, 308, limit cycles during simultaneous 338-344,578-580 C O and 479 over platinum, carbon monoxide 475 Pellet(s) catalyst 462 process, computer-aided develop­ -filled crossflow monolith 83-85 ment of the cyclohexane 348 mathematical model for reaction in process, improvement of the C H - 349 partly wetted catalyst 391 reactions 63 partially wetted catalyst 389 catalytic partial 215 thermal conductivity of a 191 section by means of T I S F L O , Penultimate effect kinetics 175 simulation of a plant 352 420 of sodium sulfite 154 Percolation theory of S 512,582 Perforated plate columns of large diameter, axial mixing of liquid steady state multiplicity during C O 477 in 337 tubular reactor for xylene 19 Oxygen 477, 488 Performance of industrial reactions 571 Periodic effluent concentrations 534 Ρ Periodic effluent hydrocarbon distri­ P ( O C H ) isomerization 44 butions, steady state and 529 Packed bed(s) 248,250 Periodic operation 520-523 2 3 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 INDEX 613 Permeability 437 Perturbation(s) collocation method 232-235 of the initial steady state, deliberate 468 method 564 single inlet concentration 461 solution for small times 229 transient behavior of the reactor for finite 568 Phase deviation from plug flow, liquid 387 Phase, equilibrated gas 583 Phenomenon, early-late reaction zone 559 Phi-factor kinetics 175 Physical component, azimuthal 73 Physical dimensions of crossflow monoliths 84 Pilot plant, adiabatic data 29 Pilot plant, isothermal fixed-bed reforming 287 Pilot-reactor, mini37 Pilot unit scale reactor 577 Piston-flow region 404-406 Plane, Nyquist 566-569 Plant experiments, comparison of loop reactor data with pilot 24 Plant oxidation section by means of T I S F L O 352 Plant reactor 25, 574, 575 Plant scale reactor 574 Plastic powders, nonporous 193 Plate(s) on axial mixing, effect of 345 efficiency 346 method, modified 194 Platinum 477 -alumina catalyst 463, 466 carbon monoxide oxidation over 475 catalyst, catalytic oxidation reactions over supported 475, 476 Plot(s) Arrhenius 310,583,586 of conversion vs space velocity 69 for oxidation of ethylene, Arrhenius 77 of reaction rate with gas composition, Arrhenius 587 of selectivity vs conversion 520 between the specific growth rate, reciprocal 167 of yield vs conversion 520 plug flow 72, 425 of liquid 387, 388 model 242-244 axially dispersed 239 reactor 254,337,428 tubular reactor with high heat diffusivity 562 Plugging, pure pore mouth 202-205, 254 Plugging time, analytical evaluation of the 228 Poincaré theorems Poiseuille profile, laminar Poison (ing) deposition mode of deactivation in monolithic catalysts nonselective pure selective Polymer concentration Polymer molecular weight Polymerization Polynomials, legendre Pore blockage diffusion 487 72 115 202 110 110-111,115 205 111-115 143 173 140,173 542 232 226 desulfurization 254 mouth plugging, pure 202, 205 plugging model 225,226,231-235 for gas-solid reactions 225 size 584 structure and foulant deposit geometries 201, 202 internal 391 model 203 of the particle, diffusional resistance through the 225 Porosity changes 225 Powders, nonporous plastic 193 Prandtl's number, (Pr) 45,248 Precipitation 591 Pressure apparatus 314 of C , liquid phase partial 369 of carbon monoxide, partial 30 change, system response to 56 drop equation 271 ketone vapor 421 response characteristics 55 transducer 53 transient for ferf-butanol catalytic dehydration, adsorption-reaction 58 Probability for a particle, escape 572 Problems, stability 539 Product, diffusional resistance through the solid 225 Product gas, recirculation cold 63 Profile(s) analytic solution for nonuniform viscous flow, velocity 149 axial 360 flow, steady state temperature 552 in the catalyst bed, concentration 67 composition 288 concentration 230,261 description of measured 366 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 614 CHEMICAL REACTION ENGINEERING—HOUSTON Profile(s) (continued) for different thermal conductivities, mole fraction 102 in the entrance region of a monolithic convertor 72 ethylene concentration 535 exit 144 gas 368,369 gas phase 365 heat flux 271 initial velocity 144 inlet velocity 144 isothermal reforming reactor 289 laminar Poiseuille 72 mixed flow 220 in multiple channels, radial temperature 107 paraffin and benzene compositio region of multiplicity, upper lower temperature 546 solid temperature 116 steady state 559 temperature 144, 239,240, 246,514, 540 transient behavior of temperature 560 tubeside temperature 220 tube wall temperature 271 Program description, computer 54 2-Propanol Propanol, aeration of 377, 378 over alumina, dehydration of 10 Properties of catalysts 195,462 Properties, fluid dynamic 362 Proportional control 563 Pseudomonomolecular kinetic reforming model, realtime activity parameters of a 282 Pseudosolubility 153 Pulse amplitudes 468-471 Pulse duration on conversion enhancement, effects of 468-472 Pulsing at various temperatures 469 Pump, metal bellows recycle 476 Pyrolysis of ethylbenzene 313-316 Pyrosulfonic acid 327-329 Q Qualitative trends of the hysteresis curve Quartz 99 314 R Radial conductivity 247-250 dispersion effects 363 distribution of fractional sites 116 distribution of poison deposition 115 flow 550-554 inlet 541 mixing 304-306 Radial (continued) Peclet numbers 242 temperature profiles in multiple channels 107 Radiation 273,276 Radiative heat transfer 273 Radical reaction equations 350 Raphson algorithm, Newton88 iteration, Newton114 method, Newton103 Rasching rings 339 Rate(s) on axial mixing, effect of gas flow 342 of C O conversion 492 constant(s) effect of coke deposition on reaction 310 realtime activity 283 of conversion 38 determination of, reaction 22 equation(s) 23 intrinsic 416 parameters, activation energies and frequency factors 22 reaction 414 as a function of product sulfur, reaction 454 with gas composition, Arrhenius plot of reaction 587 gas-exchange 401,441 glucose consumption 170 growth 163 intrinsic mass transfer 13 molar gas flow 360 of oxidation of S over vanadium oxide 512 on performance, effect of agitation 452 reaction 457 shear 149 static global of sublimation 8, superficial liquid velocity dependence of reaction 415,418 transient global Ratio, recycle 17 Reactant(s) feed system 513 mass transfers, representation of 418 nonvolatile liquid 388 species, concentration of a 441 system reaction, single 57 Reaction(s) adsorption to the catalyst bed, concentration changes caused by 68 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 INDEX 615 Reaction(s) (continued) catalytic partial oxidation 215 conditions, adsorption at 57 development of reaction models for complex gas phase 313 effect of periodic operation on the selectivity of catalytic 512 equation(s) with the Damkohlen number 76 radical 350 with the Schmidt number 76 first-order irreversible 388 first-order steady-state chemical 402 gas-phase 4,447 gas-solid noncatalytic 226 heat adsorption, types of 63 of hydrocarbons, thermal decomposition 31 hydrocracking 306,30 kinetic modeling for oscillatory catalytic 487 in the liquid phase, micromixing phenomena in continuous stirred reactors 125 mass transfer in absorption without 329 mechanisms 309,488 models for complex gas phase reactions, development of 313 noncatalyst homogeneous liquid phase 388 oxidation 63 in partly wetted catalyst pellets 391 pore plugging model for gas-solid 225 rate(s) 457 Arrhenius diagrams for 31 of carbon monoxide, reduced 30 on the catalyst 217 constants 310 determination of 22 equation 414 as a function of product sulfur 454 with gas composition, Arrhenius plot of 587 superficial liquid velocity dependence of 415, 418 temperature dependency 30 regime of mass transfer with chemical 327 selectivity 574 studies, adsorption 57 over supported platinum catalyst 475, 476 tube wall catalyzed 74 vapor-phase catalytic 293 zone phenomenon, early-late 559 Reactor(s) adsorber50-53,59 backmixed 309 bench-scale 303 coated tube 63 Reactor(s) (continued) cocurrent 218-222 gas-liquid tube 329 components 51 conditions during comparisons of trickle and batch operations 432 configurations, comparison of 217 continuous flow spinning basket stainless steel 527 continuous flow stirred tank 337,430,498 coolant pass 221 countercurrent 218-220,414 cyclone 328-334 design features 17, 51, 540 development 50,450 differential 10,15 evaluation 50 fixed bed 513,539 fluidized-bed 563 gas-liquid 352,353 glass tubular 207 Gulf-patented segmented bed 304 -heat exchanger 83,89-93 honeycomb 77 impinging jet infrared cell-recycle ir cell 4, 5,10,11 inlet temperature 282,288 integral 15-17,22, 462 internal recycle 26 isothermal 72,512,526 laboratory 16 liquid full upflow 428 loop 15-25 mini-pilot 37 mixed flow 219 model(s) fluidized 436-438 gas-liquid 351 multitubular 215 slugging fluidized bed 400 trickle-bed 411 monolithic (active wall) 72 moving bed 543 multiphase spinning basket 449 multiplicity wall-catalyzed 98 multitubular 215 parallel passage 63-70 performance of industrial 571 pilot unit scale 577 plant 474,575 plug flow 254,337,428 prototypes, cell recirculating batch recirculation 583 selectivity in 331-333 single-wafer catalytic recycle 13 spinning basket 448 stirred cell 328-334 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 CHEMICAL REACTION ENGINEERING—HOUSTON 616 Reactor(s) (continued) trickle-bed 414-416,447 trickle flow 431 tube 15-17,219,334,512 Realtime activity kinetics 287, 288 Realtime activity parameters 282,283 Recirculation reactor 583 Recycle flow 584 pump, metal bellows 476 ratio 17 reactor impinging jet infrared cell3 internal 26 single-wafer catalytic 13 Reduction of ores, hydrogen 440 Reduction, vanadium 585, 591 Regime, kinetics of the liquid diffusion 59 Residence time 337, 516, 527 analysis 571 curves, concentration20 data 573-579 density 572-579 distribution 339-341,571, 576-580 Residue, Caribbean 255-262 Residues, Middle East 255-262 Resistance, kinetic 225,230 Resistance, liquid diffusion 592 Reynolds number 8, 45, 89, 243-249, 465 Rings, Pall 339,344 Rings, Rasching 339 Rosenbrock's parameter search technique 287 Rotameters 507 Run(s) 90-93 cyclic 517 Runaway analysis ( R A ) 175-183 Runge-Kutta methods 315 technique 90 variable step size integration routine 103 Ruthenium catalyst 411 S Scanning calorimetry, differential 181 Scans, steady-state spectral 12,13 Schmidt method, Binder— 67 Schmidt number 75, 76 Selective poisoning 111-115 Selectivity of catalytic reactions, operation on the 512 on C O conversion, dependence of 28 vs conversion, plot of 520 conversion, yield 514 in the cyclone reactor 333 Selectivity (continued) effects 557 of catalyst pretreatment of 35 ethane 531 influence of mass transfer on 327,328 matrix 284 under periodic operation 521-523 rate constant matrix 285 reaction 574 steady state 519 in stirred cell reactor 331 of straight chain hydrocarbons 34 in the tube reactor 333 Semenov-type dimensional analysis 173 Sensitivity analysis 353 limitations, monomer 175 Shear rate 149 Sherwood numbers 99 Shrinking aggregate model 130 Simplex method (Nelder and Mead), derivative-free 22 Simpson's integration rule 286 Single reactant system reaction 57 Single-wafer catalytic recycle reactor 13 Sliding thermocouple 412 Slugging fluidized bed reactor 400, 404 Sodium hydroxide 339 Sodium sulfite, oxidation of 154 Solid contact and mixing gas51 interface, fluid— 115 interface, l i q u i d 428 reactions, pore plugging model for gas225 systems, gas— 554 thermal conductivity 101 transport, l i q u i d 393 Solvation, coal 304-310 Space velocity conversion vs 68, 69 Spectra, surface 3, Spectral scans, steady-state 12,13 Spectrometer ir 3-7 magnetic-deflection mass 477 time of flight mass 314 Spinning basket reactor 447-449 stainless steel, continuous flow 527 Spray column, liquid/liquid 539 Stability 551 of controlled reactor 565 diagrams 501-504 domain 567-569 parameter 564 problems 539 steady state 499, 566 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 617 INDEX Stainless steel reactor, continuous flow spinning basket 527 Start-of-cycle reactor inlet temperatures 282 Static conductivities 249 global rates methods 190,195 process 248 surface spectra Steady state for 2% C O , multiple 480 compositions 528 continuity equation 73 conversion of C H 518 conversion performance with puls­ ing at various temperatures 469 diagrams 56 equation 492 gas analyses 513 hysteresis in the conversion-inlet temperature domain 467 methods 339 multiplicity 98, 466, 477 profiles 559 runs 517 selectivity 519 spectral scans 12,13 stability 499,566 temperature 532, 563-567 yield of C M 519 Stirred cell reactor 328-334 aromatic sulfonation in a 327-329 selectivity in 331 Stirred tank experiments 262 reactor 4, 430 catalyst life in a 260 continuous flow 125, 337, 498 metal removal in a 260 self-sustained oscillations in a 498 Solubilities, gas 593 Stokes-Einstein equation 331 Stokes equation of motion, Navier- 72, 73 Styrene 315-323 -acrylonitrile ( S A N ) 175 -methyl methacrylate ( S M M A ) 175 Sulfite, oxidation of sodium 154 Sulfide deposits, metal258 Sulfonation aromatic 327 of benzene 327,334 experiments 329-333 mass transfer 329 Sulfovanadate complexes 582 Sulfur 425 concentration 255 dioxide absorption of 225 4 dioxide (continued) oxidation kinetics over vanadium oxide, rate of oxidation of reaction rate as a function of product trioxide Sulfuric acid Synthesis of ammonia, catalytic Synthesis, Fischer-Tropsch Technological Information System (TIS) Temperature(s) amplitude, stability diagram of 582 512 454 327-332 359 550 26,63 352 504 distribution of Ο 118 cell number after a shift in 169 coefficient of sensitivity 53 comparison of some representative amplitudes of 505 control of methanation reactors 63 conversion of ethane gas inlet 546 and conversion, measured oscilla­ tions of 508 dependence of "heat transfer property" γ 47 dependency, reaction rate 30 for different wall thermal conductivities 101,102 distribution, integral reactor 21 domain, steady state hysteresis in the conversion-inlet 467 extinction 98 ignition 98 inlet gas 544 lag 57 in multiple channels, wall 105-106 oscillation of 480-483, 501-503, 568 profile( s ) 144, 219-221, 240, 246, 514, 540 axial flow 552 in multiple channels, radial 107 radial 239 region of multiplicity, upper and lower 546 transient behavior 560 tube wall 271 solid 116 tubeside 220 programmed run, diazo-decomposition's 42 reactor inlet 282, 288 shift on growth, effects of 168 specific growth rate at varying 166 steady-state 469, 463-567 transient behavior of reactor 569 variations, gas phase 479 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 CHEMICAL REACTION ENGINEERING—HOUSTON 618 Termination models 174 Theorems, Bendixon 487 Theorems, Poincaré 487 Theory Langmuir monolayer 516 percolation 420 residence time distribution 571 true volume ideal two-phase 438 two-phase 436 Thermal conductivity 190-195,315 mole fraction profiles for different 102 of a pellet 191 of porous catalysts 189 solid 101 temperatures for different wall 101,102 cracking furnace 271-274 data decomposition reactions of hydrocarbons 313 design data from a bench-scale heatflow calorimeter 37 energy balance 173 hazard(s) 43-45 ignition 173 ignition point apparatus 182 instrumentation 37 liquefaction processes 303 methods 37 phenomena in chain addition copolymerization 173 runaway ( R A ) 173,182 Thermocouple ( s ) 17, 53, 57 axial 412 Cr/Al 238 sliding 412 Thiele modulus 34,99, 125 Thiophene 207 Thodos correlation, de Acetis466 Thomas method 143 Time analysis, residence 571 -averaged conversion 505 -averaged model 408,409 curves, concentration-residence 20 data, abstract residence 573 density function, residence 572 distribtuions, residence 339 of flight mass spectrometer 314 lag 568,569 bacterial 172 influence of 566 residence 337,527 testing of the plant reactors, residence 574 Toluene 288,315,316 Transfer, mass 8,13-15,153,154, 388 in absorption without reaction 329 in a bubble column, C0 -interphase 359 Transfer, mass (continued) with chemical reaction, regime of 327 coefficient 311,365-367 effects 306 gas-liquid 387 representation of reactants' 418 on selectivity, influence of 327,328 in stirred cell reactor during sulfonation 329 in a trickle-bed reactor 420 Transformation, LaPlace340 Transient analysis 559 Transient behavior of reactor temperature 568-560 Transition, R A 179,183 Transport to the catalyst bed, concentration equation, mass 73 isotropic 420 liquid-solid 393 of vorticity, convective 74 Trickle-bed reactor 416 butanone hydrogénation in 413 catalyst effectiveness factor in 387 countercurrent 414 model 411 of the liquid distribution in a 417 of mass transfers in a 420 performance equations for 389 Trickle flow and batch operation, comparison of 432, 433 reactor 431 catalyst utilization in a 425 Tropsch synthesis, Fischer63 Truncation on catalyst effectiveness, effect of matrix 393 Tube -particle diameter ratio 238 reactor 334 aromatic sulfonation in a cocurrent 327 cocurrent gas—liquid 329 selectivity in the 333 wall-catalyzed reaction 74 wall temperature profile 271 Tubeside temperature profiles 220 Tubular reactor(s) 15-19,63,512 glass 207 with high heat diffusivity, flow control operation of a plug-flow 562 limitations 149 polymerization in a 140 Turbulant conduction 248,249 Two-phase model 359,400-403, 539 Two-phase theory, true volume ideal 438 Two plate method 191 In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 619 INDEX U U , hydrofluorination of Upflow reactor, liquid full Utilization, experimental system for determining maximum catalyst 440 428 429 V2O5-K2S2O7 catalyst, oxidation of S on supported molten 582 Valualdehyde 294-298 Vanadium 255-259, 588, 592 oxide, rate of oxidation of S over 512 removal 261-263 reduction 585, 591 Vapor phase catalytic hydrogénation 526 Vapor phase catalytic reaction Vapor pressure, ketone 42 Variability, intensity function representation of residence time 571 Vector, vorticity 73 Velocity conversion vs space 68,69 dependence of reaction rates, superficial liquid 415-418 in the entrance region of a monolithic convertor 72 field development, axial 76 and "fines" content, interstitial flow increases with gas 439 fluid interstitial 551 gas linear 375-380 profiles 75,144,149 Viscous flow, velocity profile analytic solution for nonuniform 149 2 Wall biot number 242,249-251 -catalyzed reaction 74 -catalyzed reactors 72,98 thermal conductivities 101 Water displacement method 513 Water on ierf-butanol adsorption, effect of 58 Watson kinetic models, Hougen and 57 "Wedge layering" model 202,211 Wetted catalyst pellets 391 Wetted slab 394 Wetting efficiency 411 external 390,391 incomplete catalyst 427 internal 390 X Xylene, aeration of 377,378 Xylene oxidation, tubular reactor for 19 Y Yield vs conversion, plot of conversion, selectivity ethane as function of cell number, fractional under periodic operation, mean and selectivity under periodic operation 517 520 514 532 558 521 523 Ζ W Wafer catalytic recycle reactor, single- 13 Zeolite cracking catalysts Ziegler catalysis Zone, ignition In Chemical Reaction Engineering—Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 288 140,149 101 ... Reaction Engineering, 5th, Houston, Tex., 1978 Chemical reaction engineering? ? ?Houston (ACS symposium series; 65 ISSN 0097-6156) Bibliography: p Includes index Chemical engineering? ??Congresses Chemical. .. diagram for reaction rates In Chemical Reaction Engineering? ? ?Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 CHEMICAL REACTION ENGINEERING? ? ?HOUSTON. .. ensure maximum In Chemical Reaction Engineering? ? ?Houston; Weekman, V., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1978 In Chemical Reaction Engineering? ? ?Houston; Weekman,