OP-II-3

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PP-I-15THE MECHANISM OF SELF-OSCILLATIONS GENERATION IN CSTR.CONSECUTIVE REACTIONDeyun Е.V., Andrianova Z.S., Kustova L.V., Samoilenko N.G.,Korsunskiy B.L.Institute of Problems of Chemical Physics of the Russian Academy of Sciences.Academician Semenov avenue, 1, 142421 Moscow region, Chernogolovka, Russia.E-mail: kors36@mail.ruThe mechanism of self-oscillation generation and damping in CSTR with twoconsecutive exothermal first order reactions has been studied. It has been shown,that in the system with only one steady state oscillations arise “softly” on the lowerborder of self-oscillatory modes (small values of Semenov parameter) but on theupper border (great values of Semenov parameter) oscillations damp "rigidly", i.e. thestable limiting cycle merges with an unstable one.For adiabatic reactor the impossibility of existence of the closed trajectories inphase space has been proved.In contrast to autocatalytic and concurrent reactions, in the case of consecutivereactions the occurrence not only оf one and three, but also of five steady states isprobable. The area of five steady states arises inside of the area of three steadystates. When the relationship between activation energies of separate stages ischanged the part oh this area penetrates through the upper border turning into anadditional subarea of three steady states.The mechanism of self-oscillations generation for the cases of three and fivesteady states has been investigated. For the purpose in parametrical space Se - Da(Se – Semenov criterion, Da – Damköhler criterion) the areas of steady statesmultiplicity have been calculated. The analysis of steady states transformation andself-oscillations generation inside multiplicity areas has allowed proposing themechanism of a "rigid" birth of a stable limiting cycle (a mathematical image of selfoscillations).This mechanism is founded on the formation of saddles-knotstrajectories loop.246
PP-I-15The qualitative picture of stable limiting cycle formation for the system with threesteady states is presented on the figure.247
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Boreskov Institute of Catalysisof t
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INTERNATIONAL SCIENTIFIC COMMITTEEV
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SILVER SPONSORThe organizers expres
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PL-1HOW TO DESIGN OPTIMAL CATALYTIC
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MULTIFUNCTIONAL DEVICES FOR INTENSI
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PL-3DESIGN OF CATALYTIC PROCESSES F
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PL-3Indeed preparation and testing
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PL-4The second part of the lecture
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PL-5Reactor designs with intensifie
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PL-6MEMBRANE REACTORS: STATE OF THE
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KEY-NOTE PRESENTATIONS
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KN-1description, that can be charac
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KN-2selective catalytic reduction o
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KN-3Fig. 1. Experimental burner of
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KN-4~200°C. This is based on the H
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KN-5for addressing the quality of t
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KN-6reaction with ethanol and the b
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KN-7at temperature lower than 873K,
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REACTION KINETICS AND REACTION ENHA
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OP-I-2RELATION BETWEEN THE ACTIVATI
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COMPARISON OF CHEMICAL AND ENZYMATI
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OP-I-4NONLINEAR PHENOMENA DURING ME
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OP-I-5SPECIFICITY OF THE OSCILLATIO
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OP-I-6TRENDS IN BISTABILITY DOMAINS
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OP-I-7NON-STEADY-STATE CATALYST CHA
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OP-I-8TRANSIENT KINETIC STUDIES OF
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OP-I-9A REDOX KINETICS FOR THE PART
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OP-I-9500Flow of Air = 0.3 m 3 (STP
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OP-I-11ELUCIDATION OF THE REACTIVIT
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KINETIC MODELLING OF THE JOINT TRAN
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OP-I-13n-HEXANE SKELETAL ISOMERIZAT
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OP-I-14the slow branch of kinetic c
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OP-I-15The hydride palladium comple
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Energy Conservation (field j)∂∂
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OP-I-17Selectivity (mol. %)10099989
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OP-I-18According to GLC the main pr
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OP-I-19and slug dimensions, formati
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OP-I-20A RANS volume of fluids [1]
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OP-I-21the physical-chemical charac
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OP-I-22calculated values of pressur
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OP-I-23where L c - capillary length
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OP-I-24and diffuse transmission thr
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OP-I-25effect of bubble break-up wo
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OP-I-26strong influence on the soli
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OP-I-27wHCOOH=1+K2K1(1 + K3⋅ P⋅
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OP-I-28dimensional profiles detecte
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OP-I-29results. The results of the
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OP-I-30Fig. 1. Hydrodynamics and co
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OP-I-31Convection and diffusion wit
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TEMPERATURE RISE DURING REGENERATIO
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OP-II-2[4]. Similar temperature pro
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OP-II-3(Fig, 1 a, b) upon testing i
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OP-II-4In the second step optimizat
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OP-II-5membrane contactors were stu
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OP-II-6reaction over Cu/CeO 2-x cat
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OP-II-7is modelled by means of a tw
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OP-II-8the reactor [6]. However, th
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OP-II-9Figure 1. Computed volume fr
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OP-II-10assumes variables’ distri
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OP-II-11oxide support, it comes tha
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OP-II-12was connected to G.C. via s
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OP-II-13catalyst bed was 6 mm. Thre
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OP-II-14as coolant is an important
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OP-II-15Flow (L/h)7654321Bottoms ra
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OP-II-16(4) The gas recirculation r
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OP-II-17Catalytic reactions were ca
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OP-II-18At steady surface coverage
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OP-II-19gaimpulsegeneratorwateFig.
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OP-II-20examined (see Figure 1). Th
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OP-II-21References[1]. M.P. Dudukov
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OP-II-22of the hydrogen oxidation a
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OP-II-23TemperaturesensorsThe efflu
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OP-II-24of reactant conversions. Pa
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OP-II-25(surface) ‘wall-reaction
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OP-II-26It was found that the 10 wt
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OP-II-27non-flow type. During the M
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OP-III-A-1A NEW SIMPLE MICROCHANNEL
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BUBBLING FLUIDISED BED PYROLYSIS OF
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PINEWOOD PYROLYSIS UNDER VACUUM CON
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OP-III-A-5PYROLYSIS OF HDPE IN A CO
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OP-III-A-6REACTORS FOR THE GREEN TR
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DEHYDRATION OF GLYCEROL TO ACROLEIN
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OP-III-A-8LACTIC ACID BASED ON BIO
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RECOVERY OF ACETIC ACID FROM PYROLY
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OP-III-A-10LIPASE-CATALYZED REACTIO
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OP-III-A-11INVESTIGATION ON THERMOC
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OP-III-A-12SELECTIVE CATALYTIC DEOX
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ETHANOL STEAM REFORMING OVER COBALT
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OP-III-A-14HYDROTREATMENT CATALYSTS
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ORAL PRESENTATIONSSECTION IIIChemic
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OP-III-B-1Reactor parameters:Intern
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OP-III-B-2JOINT STEAM REFORMING OF
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OP-III-B-3LANDFILL BIOGAS PURIFICAT
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OP-III-B-4MODELING AND SIMULATION O
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OP-III-B-5DemonstratorThe medium-te
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OP-III-B-630/19.6 Nl/min (space vel
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OP-III-B-7mixed in the ratios: 94,8
Page 195 and 196: OP-III-B-8Table 1.Material balance
Page 197 and 198: OP-III-B-9Based on the results of t
Page 199 and 200: OP-III-B-10On this basis it can be
Page 201 and 202: OP-III-B-11Similar trends caused by
Page 203 and 204: OP-III-B-12(mol/s g cat)x108r4,6-DM
Page 205 and 206: OP-III-B-13carbon in Wyoming coal i
Page 207 and 208: OP-III-B-14MODELING PRODUCT DISTRIB
Page 209 and 210: OP-III-B-15COMBINED TECHNOLOGY OF U
Page 211 and 212: MATEMATICAL MODEL FOR DOWNDRAFT BIO
Page 213 and 214: OP-III-B-17CATALYTIC DEHYDRATION OF
Page 215 and 216: OP-III-B-18SYNGAS AND HYDROGEN PROD
Page 217 and 218: POSTER PRESENTATIONSSECTION I
Page 219 and 220: PP-I-1influence of the direction of
Page 221 and 222: PP-I-2At the agitation of the liqui
Page 223 and 224: PP-I-3NOLINEAR PHENOMENA IN CATALYT
Page 225 and 226: PP-I-4A NEW APPROACH TO KINETIC STU
Page 227 and 228: PP-I-5KINETICS OF PROX REACTION OVE
Page 229 and 230: PP-I-6PHENOMENA OF SUPERADIABATIC T
Page 231 and 232: ELECTROMAGNETIC REACTOR OF WATER TR
Page 233 and 234: PP-I-8DIRECT SYNTHESIS OF HYDROGEN
Page 235 and 236: PP-I-9DYNAMICS OF FIRST-ORDER PHASE
Page 237 and 238: PP-I-10ELECTROCHEMICAL OXIDATION OF
Page 239 and 240: PP-I-11CHEMPAK SOFTWARE PACKAGE: OP
Page 241 and 242: PP-I-12COMPUTER SIMULATION OF ENDOT
Page 243 and 244: PP-I-13MODELLING KINETICS OF PROCES
Page 245: PP-I-14THE INVESTIGATION OF REACTIO
Page 249 and 250: Thus, knowing the composition of ra
Page 251 and 252: PP-I-17current density. Preliminary
Page 253 and 254: PP-I-18Hydrogenation kinetics was d
Page 255 and 256: PP-I-19the active mixing, amplitude
Page 257 and 258: PP-I-20where r, h indicate the radi
Page 259 and 260: PP-I-21model is very anisotropic be
Page 261 and 262: PP-I-22- Reduction of the number of
Page 263 and 264: PP-I-23oscillations of intermediate
Page 265 and 266: PP-I-25SYNTHESIS OF ETHYLENE OXIDE
Page 267 and 268: PP-I-26OPTIMUM KINETICS FOR POLYSTY
Page 269 and 270: PP-I-27TableSpecific surface area (
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Page 273 and 274: PP-I-29commercial CFD solver FLUENT
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Page 277 and 278: PP-I-31The destruction ways of CF 3
Page 279 and 280: PP-I-32[7]. Karoor S, Sirkar K. Gas
Page 281 and 282: PP-I-33above 750°. The catalytic p
Page 283 and 284: PP-I-35REVERSE FLOW REACTOR WITH FO
Page 285 and 286: FLOW-RECIRCULATION METHOD FOR INVES
Page 287 and 288: TO A PROBLEM OF OPTIMIZATION OF FUN
Page 289 and 290: PP-I-38THE INFLUENCE OF REACTION MI
Page 291 and 292: PP-I-39METHANOL OXIDATIVE STEAM REF
Page 293 and 294: PP-I-41CORRECT INVESTIGATION OF THE
Page 295 and 296: PP-I-42NEW APPROACH OF DEFINITION O
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PP-I-43STREAM HEAT EXCHANGE OF AERO
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PP-I-44HIGH TEMPERATURE OXYGEN TRAN
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PP-I-45KINETICS OF TRANSESTERIFICAT
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MATHEMATICAL MODELING AND OPTIMIZAT
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PP-I-47The basic side reaction is r
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PP-I-49EXPERIMENTAL STUDY OF THE HA
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PP-I-51ON THE KINETICS AND REGULARI
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PP-I-52DIFFERENTIAL THERMAL ANALYSI
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PP-I-53oxidation reaction demonstra
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PP-I-54of reaction. It is establish
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PP-I-55effects, are energetically c
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PP-I-56The experiments and simulati
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PP-I-57In the studied range of temp
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PP-I-58HeadingsAdvances in Chemical
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PP-I-59calculated. During the aroma
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PP-I-60with honeycomb catalyst) act
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Т - temperature, K, D eff - effect
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PP-I-62stirring rate were adopted u
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PP-I-63m 2 = (k 1 y 0 1 +k -1 +k 1
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POSTER PRESENTATIONSSECTION II
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PP-II-1values of operating paramete
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⎡⎛⎢⎜bF⎣⎝=2ab ⎞ 6+ ⎟
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PP-II-4HONEYCOMB MONOLITHIC CATALYS
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MATHEMATICAL MODELING OF THE ALUMIN
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PP-II-6MODELING OF VINYL ACETATE SY
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PP-II-7СENTRIFUGAL DISK REACTORAvv
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PP-II-83) An opportunity of operati
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PP-II-10UV-ACTIVATION OF METHANE CO
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PP-II-11COMBINED APPROACH (FMEA- HA
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PP-II-12Testing the pilot variant o
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PP-II-14NOVEL MICROREACTOR FOR THE
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PP-II-15of 1-2.5 lead to a decreasi
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PP-II-16stages. Kinetic parameters
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PP-II-17whiskers, which assure an a
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PP-II-18с m , с cat - density of
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PP-II-19decrease. So, the potential
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PP-II-20products became a mixture o
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PP-II-21A numerical algorithm and s
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PP-II-22motions at any external con
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PP-II-23One of the main technologic
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PP-II-24100 m x 250 μm x 0.5 μm,
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PP-II-25A model was developed to ca
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PP-II-26The results of calculations
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PP-II-27modes of reaction and two d
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PP-II-29OZONE-DESTRUCTION REACTOR B
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PP-II-30Fig. 1. Axial profile of me
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PP-II-31isobutylene in butene fract
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PP-II-322.5x10 -3 ( i )2.5x10 -3 (
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PP-II-33No olefinreadsorptionWith o
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PP-II-34using titania or Ag-doped t
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PP-II-35accidents, is condition dep
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PP-II-36be seen that at temperature
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PP-II-37the solid phase solute conc
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PP-II-38As shown in Table 1, the ca
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PP-II-39better to the obtained in t
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PP-II-40Hydrodynamic regime in the
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PP-II-41activity, relative unit1,21
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PP-II-42One of the major indicators
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PP-II-43These conditions are confor
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PP-II-44For the hepten, alpha-methy
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PP-II-46PARTIAL OXIDATION OF METHAN
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PP-II-47DEVELOPMENT OF VORTEX APPAR
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MODELING OF CFTALYTIC α-OLEFINS OL
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PP-II-49Hinselwood kinetic equation
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3) iterate concentrations at a cut
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PP-II-51data such flow sheet provid
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PP-II-53ON THE TECNOLOGY OF TECHNIC
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PP-II-54PROPYLENE POLYMERIZATION AN
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REACTOR FOR LIQUID-PHASE PROCESSES
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PP-II-56MODELING OF CATALYTIC MICRO
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PP-II-57MATHEMATICAL MODELING OF BE
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PP-II-58HONEYCOMB CATALYSTS WITH PO
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POSTER PRESENTATIONSSECTION IIISECT
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ReferencesPP-III-1[1]. A.N. Pestrya
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PP-III-2Table1. Percentages of diff
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PP-III-3conversion for the reaction
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PP-III-4900Reformer temperature (K)
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PP-III-5Catalytic performance of th
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PP-III-6optimization permit better
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PP-III-8DE-NO X SYSTEM BASED ON H 2
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PP-III-9SEPARATION BETWEEN CHLORIDE
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CONVERSION OF WASTE COTTON TO BIOET
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PP-III-12THE METHOD OF GLYCERIC ACI
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NOx conversion vs. temperature is p
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PP-III-14intermetallic diffusion at
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PP-III-15The conversion of O 2 was
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PP-III-16H 2consumpition (a.u)(a)39
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PP-III-17the characteristic structu
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PP-III-18Figure 1. Influence of tem
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PP-III-19(a)(b)CH 4conversion, %100
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PP-III-20take into account own size
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PP-III-2110080CS-18CS-34CHZ30CHZ801
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EXPERIMENTALPP-III-22We synthesized
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PP-III-23Base composition component
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PP-III-25CO REMOVAL AT THE MICROSCA
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HYDROGEN PRODUCTION FROM METHANOL U
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PP-III-27NON CATALITIC PRODUCTION O
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PP-III-28Different reaction conditi
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PP-III-29followed by WGS reaction.
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PP-III-30As a solvent-coreactants w
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PP-III-31It was concluded that on t
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PP-III-32Hydrogenolysis of glycerol
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PP-III-331,6W 0, μmol Н 2/min1,20
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PP-III-34preparation (glass fiber f
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PP-III-35In the modification proces
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PP-III-36The kinetics of acid hydro
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PP-III-37reaction: i) C=O double bo
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PP-III-38methane and carbon monoxid
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PP-III-39from 25 to 60, which was d
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PP-III-401% w/w for Pd with respect
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PP-III-41material. Besides, the mol
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PP-III-43METHANOL AND DIMETHYL ETHE
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PP-III-44goal is attained by using
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OLIGOMERISATION OF TERTIARY AMINE L
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PP-III-47meter (Shimazu Co.; TOC-50
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PP-III-48the range of 29-87 kJ/mol
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PP-III-49determine the optimal type
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PP-III-50NEW CONCEPT FOR A SELF CLE
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PP-III-51HYDROGEN PRODUCTION BY MET
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PP-III-52CATALYTIC UPGRADING OF PRO
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PP-III-53CATALYTIC CONVERSION OF FI
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PROCESS FOR THE PRODUCTION OF BUTYL
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PP-III-55been previously fixed and
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PP-III-56The influence of reaction
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PP-III-57sample does not contain so
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PP-III-58The re-activation of the e
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PP-III-59The aim of this work is th
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PP-III-61BIODIESEL FROM MICROALGAE
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DEVELOPING MICROFLUIDIC DEVICE WITH
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THREE-PHASE DIRECT OILS HYDROGENATI
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Co-BASED CATALYSTS FOR THE HYDROLYS
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PP-III-65KINETIC STUDY OF THE CATAL
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PP-III-66PRODUCTION OF HYDROGEN AND
Page 563 and 564:
PP-III-67ENHANCED GASIFICATION OF P
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PP-III-68INFLUENCE OF SPILLOVER ON
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PP-III-69AEROBIC OXIDATIVE COUPLING
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PP-III-70MECHANISMS FOR CHEMICAL RE
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PP-III-70SBS molecules and increase
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PP-III-71and as a resut, could enha
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PP-III-72conversion). Al 2 O 3 /PSS
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PP-III-73SBA50TiSBA% Transmittance5
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PP-III-74stove heating. Another par
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PP-III-75TG [%]0-10-20-30380°C400
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PP-III-76The elementary version of
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PP-III-77thermodynamically enhanced
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PP-III-78GFC textileStructuringmeta
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PP-III-79All the prepared spinel-ox
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PP-III-80Our new process is polluti
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PP-III-81Fig. 1. Scheme of the biog
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PP-III-82Pic. 1 Pic. 2Pic. 1. Schem
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ARKHIPOV Vladimir AfanasievichResea
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CENTENO Felipe OrlandoNúcleo de Ex
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FLID Mark RafailovichScientific Res
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HOSEN Mohammad AnwarUniversity of M
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KOZLOVA EkaterinaBoreskov Institute
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MAKARSHIN Lev LvovichBoreskov Insti
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ONSAN Zeynep IlsenDepartment of Che
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REBOLLAR MoisesInstituto De Investi
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SHEIKH Munir AhmedTraining and Staf
Page 615 and 616:
SULMAN Esfir MikhailovnaTver Techni
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ZHAPBASBYEV Uzak KairbekovichKazakh
Page 619 and 620:
OP-I-3 Pécar D., Gorsek A.COMPARIS
Page 621 and 622:
OP-II-3Kucherov A.V., Finashina E.D
Page 623 and 624:
OP-III-A-9 Rasrendra C.B., Girisuta
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PP-I-9Bykov V., Tsybenova S.B.DYNAM
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PP-I-43 Pechenegov Y.Y., Kuzmina R.
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PP-II-10 Basov N.L., Oreshkin I., T
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PP-II-45 Stepanek J., Koci P., Kubi
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PP-III-19 Fedorova Z.A., Danilova M
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PP-III-53 Pölczmann G., Valyon J.,
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XIX International Conference on Che
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