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ORAL PRESENTATIONSSECTION IIChemical Reaction Engineering and Reactors Design –Novel Approaches, Modeling, Scale-Up, Optimization:New Designs of Chemical Reactors (Membrane Reactors,Microreactors, Structured Reactors, etc)Novel Approaches in Chemical Reaction ProcessesEngineering (Unsteady-state and Transient Processes,Reverse-flow Operation, Sorption-Enhanced ReactionProcesses, Multifunctional Reactors, Reaction-SeparationProcesses, etc)
TEMPERATURE RISE DURING REGENERATION OF DIESELPARTICULATE FILTERSChen K., Martirosyan K.S. and Luss D.OP-II-1Department of Chemical and Biomolecular Engineering, University of Houston,Houston, Texas, USA, 77204, Dluss@UH.eduThe Diesel Particulate Filter (DPF) is the best existing technology for removal ofparticulate matter (PM). It is a wall-flow monolith consisting of many parallel extrudedsquare porous ceramic cells. Every second channel is plugged at alternate ends. Theexhaust gases enter the inlet channels and pass through the porous walls to adjacentoutlet channels. The PM accumulated in the inlet channels is periodically removed bycontrolled combustion. A major technological challenge in the operation of dieselparticulate filters (DPFs) is prevention of the occasional melting of the ceramic filtersduring regeneration (combustion of accumulated particulate matter). The cause ofthis melting is still an open question. Experiments and simulations indicate thatduring stationary regeneration (fixed feed conditions) the temperature rise is notsufficiently high to cause this ceramic Cordierite support melting (melting temperature~1250°C). The reaction engineering literature include many studies of the wrong-waybehavior in which a sudden decrease of the feed temperature to a packed bedreactor lead to a counter-intuitive temperature rise in the down stream section of thereactor. This led us to conjecture that the unexpected melting is due to a transienttemperature excursion caused by a rapid shift of the driving mode of a car fromnormal driving to idle during combustion of the particulate matter. To test thisconjecture we used Infra red imaging to measure the dynamic response of thespatio-temporal temperature on a planar DPF to a sudden change in the feedconditions. Both the experiments and numerical simulations revealed that the peaktransient temperature after the change in the feed conditions was higher than themaximal temperature of the moving regeneration front under either the initial or finalconditions. WE found that amplitude of the transient temperature rise depended onthe direction in which the soot combustion front moved in the reactor and to theperiod between the formation of the combustion temperature front and the rapidchange in the feed conditions.99
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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
Page 47 and 48: OP-I-6TRENDS IN BISTABILITY DOMAINS
Page 49 and 50: OP-I-7NON-STEADY-STATE CATALYST CHA
Page 51 and 52: OP-I-8TRANSIENT KINETIC STUDIES OF
Page 53 and 54: OP-I-9A REDOX KINETICS FOR THE PART
Page 55 and 56: OP-I-9500Flow of Air = 0.3 m 3 (STP
Page 57 and 58: OP-I-11ELUCIDATION OF THE REACTIVIT
Page 59 and 60: KINETIC MODELLING OF THE JOINT TRAN
Page 61 and 62: OP-I-13n-HEXANE SKELETAL ISOMERIZAT
Page 63 and 64: OP-I-14the slow branch of kinetic c
Page 65 and 66: OP-I-15The hydride palladium comple
Page 67 and 68: Energy Conservation (field j)∂∂
Page 69 and 70: OP-I-17Selectivity (mol. %)10099989
Page 71 and 72: OP-I-18According to GLC the main pr
Page 73 and 74: OP-I-19and slug dimensions, formati
Page 75 and 76: OP-I-20A RANS volume of fluids [1]
Page 77 and 78: OP-I-21the physical-chemical charac
Page 79 and 80: OP-I-22calculated values of pressur
Page 81 and 82: OP-I-23where L c - capillary length
Page 83 and 84: OP-I-24and diffuse transmission thr
Page 85 and 86: OP-I-25effect of bubble break-up wo
Page 87 and 88: OP-I-26strong influence on the soli
Page 89 and 90: OP-I-27wHCOOH=1+K2K1(1 + K3⋅ P⋅
Page 91 and 92: OP-I-28dimensional profiles detecte
Page 93 and 94: OP-I-29results. The results of the
Page 95 and 96: OP-I-30Fig. 1. Hydrodynamics and co
Page 97: OP-I-31Convection and diffusion wit
Page 101 and 102: OP-II-2[4]. Similar temperature pro
Page 103 and 104: OP-II-3(Fig, 1 a, b) upon testing i
Page 105 and 106: OP-II-4In the second step optimizat
Page 107 and 108: OP-II-5membrane contactors were stu
Page 109 and 110: OP-II-6reaction over Cu/CeO 2-x cat
Page 111 and 112: OP-II-7is modelled by means of a tw
Page 113 and 114: OP-II-8the reactor [6]. However, th
Page 115 and 116: OP-II-9Figure 1. Computed volume fr
Page 117 and 118: OP-II-10assumes variables’ distri
Page 119 and 120: OP-II-11oxide support, it comes tha
Page 121 and 122: OP-II-12was connected to G.C. via s
Page 123 and 124: OP-II-13catalyst bed was 6 mm. Thre
Page 125 and 126: OP-II-14as coolant is an important
Page 127 and 128: OP-II-15Flow (L/h)7654321Bottoms ra
Page 129 and 130: OP-II-16(4) The gas recirculation r
Page 131 and 132: OP-II-17Catalytic reactions were ca
Page 133 and 134: OP-II-18At steady surface coverage
Page 135 and 136: OP-II-19gaimpulsegeneratorwateFig.
Page 137 and 138: OP-II-20examined (see Figure 1). Th
Page 139 and 140: OP-II-21References[1]. M.P. Dudukov
Page 141 and 142: OP-II-22of the hydrogen oxidation a
Page 143 and 144: OP-II-23TemperaturesensorsThe efflu
Page 145 and 146: OP-II-24of reactant conversions. Pa
Page 147 and 148: 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
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OP-III-B-8Table 1.Material balance
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OP-III-B-9Based on the results of t
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OP-III-B-10On this basis it can be
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OP-III-B-11Similar trends caused by
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OP-III-B-12(mol/s g cat)x108r4,6-DM
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OP-III-B-13carbon in Wyoming coal i
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OP-III-B-14MODELING PRODUCT DISTRIB
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OP-III-B-15COMBINED TECHNOLOGY OF U
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MATEMATICAL MODEL FOR DOWNDRAFT BIO
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OP-III-B-17CATALYTIC DEHYDRATION OF
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OP-III-B-18SYNGAS AND HYDROGEN PROD
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POSTER PRESENTATIONSSECTION I
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PP-I-1influence of the direction of
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PP-I-2At the agitation of the liqui
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PP-I-3NOLINEAR PHENOMENA IN CATALYT
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PP-I-4A NEW APPROACH TO KINETIC STU
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PP-I-5KINETICS OF PROX REACTION OVE
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PP-I-6PHENOMENA OF SUPERADIABATIC T
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ELECTROMAGNETIC REACTOR OF WATER TR
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PP-I-8DIRECT SYNTHESIS OF HYDROGEN
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PP-I-9DYNAMICS OF FIRST-ORDER PHASE
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PP-I-10ELECTROCHEMICAL OXIDATION OF
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PP-I-11CHEMPAK SOFTWARE PACKAGE: OP
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PP-I-12COMPUTER SIMULATION OF ENDOT
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PP-I-13MODELLING KINETICS OF PROCES
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PP-I-14THE INVESTIGATION OF REACTIO
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PP-I-15The qualitative picture of s
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Thus, knowing the composition of ra
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PP-I-17current density. Preliminary
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PP-I-18Hydrogenation kinetics was d
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PP-I-19the active mixing, amplitude
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PP-I-20where r, h indicate the radi
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PP-I-21model is very anisotropic be
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PP-I-22- Reduction of the number of
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PP-I-23oscillations of intermediate
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PP-I-25SYNTHESIS OF ETHYLENE OXIDE
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PP-I-26OPTIMUM KINETICS FOR POLYSTY
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PP-I-27TableSpecific surface area (
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PP-I-28γ-preirradiated sample), th
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PP-I-29commercial CFD solver FLUENT
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PP-I-30modulus, a considerable decr
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PP-I-31The destruction ways of CF 3
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PP-I-32[7]. Karoor S, Sirkar K. Gas
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PP-I-33above 750°. The catalytic p
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PP-I-35REVERSE FLOW REACTOR WITH FO
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FLOW-RECIRCULATION METHOD FOR INVES
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TO A PROBLEM OF OPTIMIZATION OF FUN
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PP-I-38THE INFLUENCE OF REACTION MI
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PP-I-39METHANOL OXIDATIVE STEAM REF
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PP-I-41CORRECT INVESTIGATION OF THE
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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
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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
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SULMAN Esfir MikhailovnaTver Techni
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ZHAPBASBYEV Uzak KairbekovichKazakh
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OP-I-3 Pécar D., Gorsek A.COMPARIS
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OP-II-3Kucherov A.V., Finashina E.D
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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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