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OP-II-16MYTHOLOGY IN MULTIPHASE CATALYSIS:WHY DO THE CONVENTIONAL FIXED-BED TECHNOLOGIES HAVENO POTENTIAL FOR THE FURTHER PROCESS DEVELOPMENT?Leonid B. Datsevich 1,21 The University of Bayreuth (Germany)2 MPCP GmbH (Bayreuth, Germany)E-mail: datsevich@mpcp.de, datsevich@uni-bayreuth.deThe conventional multiphase fixed-bed (trickle-bed and bubble (packed) column)reactors are very often designated for exothermic reactions, for example, such ashydrogenation, hydrotreating, purification, the Fischer-Tropsch synthesis, etc.The contribution deals with the analysis of these reactors with regard to processefficiency, safety and design.The paper shows that these reactors do not possess any potential fordevelopment. Any attempt to improve substantially the reactor performance, e.g. toenhance the reactor productivity (not by several percent as it is always discussed inthe available literature, but by several times) cannot be realized because of therestrictions imposed by the process arrangements.The paper retraces the original ideas developed by the previous generation of theprocess developers and indicates how these ideas became the rigid paradigm thathindered the progress in the process development.The old mythology deeply established in the scientific and industrial communitiesis discussed in light of modern concepts in mass transfer and kinetics.The contribution disproves the following typical myths in the process design ofmultiphase fixed-bed reactors with a gas loop:(1) Operating pressure has to be high in order to increase the concentration ofthe gaseous compound in the liquid phase and, consequently, the reactorproductivity.(2) The reaction rate is limited by mass transfer of the gaseous compound and,therefore, operating pressure has to be high in order to enhance gas-liquid-solidmass transfer.(3) The high concentration of the liquid compound at the reactor inlet and highoperating pressure have to influence the reactor productivity nearly proportionally tothese factors if the reaction rate has the first order with respect to both gas and liquidreactants.128
OP-II-16(4) The gas recirculation rate has to be high for providing the greater gasconcentration on the catalyst surface (for speeding up the reaction rate or slowingdown the catalyst aging).(5) The gas recirculation rate has to be high for decreasing the content of bygasesin the loop (e.g. hydrogen sulfide in hydrotreaters).(6) High pressure in the reactor unconditionally encourages the slower catalystdeactivation.Some approaches towards the new process embodiments are also presented.129
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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]
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 and 98: OP-I-31Convection and diffusion wit
Page 99 and 100: TEMPERATURE RISE DURING REGENERATIO
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: OP-II-15Flow (L/h)7654321Bottoms ra
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
Page 149 and 150: OP-II-26It was found that the 10 wt
Page 151 and 152: OP-II-27non-flow type. During the M
Page 153 and 154: OP-III-A-1A NEW SIMPLE MICROCHANNEL
Page 155 and 156: BUBBLING FLUIDISED BED PYROLYSIS OF
Page 157 and 158: PINEWOOD PYROLYSIS UNDER VACUUM CON
Page 159 and 160: OP-III-A-5PYROLYSIS OF HDPE IN A CO
Page 161 and 162: OP-III-A-6REACTORS FOR THE GREEN TR
Page 163 and 164: DEHYDRATION OF GLYCEROL TO ACROLEIN
Page 165 and 166: OP-III-A-8LACTIC ACID BASED ON BIO
Page 167 and 168: RECOVERY OF ACETIC ACID FROM PYROLY
Page 169 and 170: OP-III-A-10LIPASE-CATALYZED REACTIO
Page 171 and 172: OP-III-A-11INVESTIGATION ON THERMOC
Page 173 and 174: OP-III-A-12SELECTIVE CATALYTIC DEOX
Page 175 and 176: ETHANOL STEAM REFORMING OVER COBALT
Page 177 and 178: 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
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
Page 601 and 602:
FLID Mark RafailovichScientific Res
Page 603 and 604:
HOSEN Mohammad AnwarUniversity of M
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KOZLOVA EkaterinaBoreskov Institute
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MAKARSHIN Lev LvovichBoreskov Insti
Page 609 and 610:
ONSAN Zeynep IlsenDepartment of Che
Page 611 and 612:
REBOLLAR MoisesInstituto De Investi
Page 613 and 614:
SHEIKH Munir AhmedTraining and Staf
Page 615 and 616:
SULMAN Esfir MikhailovnaTver Techni
Page 617 and 618:
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
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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.,
Page 637:
XIX International Conference on Che
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