OP-II-3

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PP-<strong>II</strong>-39POLYMERIZATION REACTOR FOR THE EVALUATIONOF CATALYSTS TYPE HONEYCOMBRebollar B.M., Silva E.Y.Instituto de Investigaciones y Desarrollo Industrial SC, Oriente 101 3605,Col Río Blanco, 07850 DF MEXICO, mrebollar@inidi.orgThere are great variety of laboratory reactors for catalysts evaluation [1,2], but inthe case of polymerization, the complications are avoided and almost all reactionsare realized are on homogeneous form. The selection of the form of the catalyst tousing in a reaction is an important stage in the design of the reactor and in thelaboratory must be the first step, normally spheres or pellets are used, but in case ofpolymerization to use this type of catalysts not always is a good idea, because duringsome polymerization reactions the viscosity varies in to large range and the level ofliquid is not constant. If mixing is not well affected at all reactor, and at every point inthe catalyst the reaction presents a low yield, due to hot spots, dead zones and a lowor even any molecular diffusion, for it the polymers industry continues using thehomogeneous reactions, assuring this way the close contact between the catalystand the reactants. To use honeycomb monolith as catalysts in the polymerizationallows a laminate flow, achieving this way a close contact with the catalyst.The designed reactor allows the evaluation of honeycomb monoliths, is of glasswith a capacity of 300 ml, the catalyst is of 1.8 x 1.8 x 0.4 cm, of square channels of1.2 mm. It can be used of constant form or for lots.The reactor was tested in the reaction of amination of the polydimethylsilxane,reaction of 24 hours for concluding [3], the catalyst was alúmina, impregnated bywashcoat with platinum, to evaluate the conversion of the reaction it was usedinfrared spectroscopy, the system was compared with the same reaction in the sametime in a homogeneous phase.The reactor was evaluated in the following concepts; Sampling and analysis ofproduct composition, isothermality, residence-contact time measurement, selectivitytime averaging disguise, molecular diffusion of the reactants in the catalystdetermining the effectiveness factor, construction difficulty and cost.The molecular diffusion was evaluated by means of the system proposed byHayes [4] and the obtained results show that the kinetic of the reaction is not limitedby its molecular diffusion, as it is confirmed by the resultant conversions that are404
PP-<strong>II</strong>-39better to the obtained in the homogeneous system. With the rest of the evaluatedconcepts the reactor shows superior qualifications to other laboratory reactors ofmajor complexity and cost, so it is confirmed the possibility of being able to use thisreactor in the evaluation of catalysts on polymerizations reactions.References[1]. Carberry J.J., Ind Eng Chem, 1964, 56, 39-46.[2]. Forni L., Catal. Today, 1997, 34, 353-367.[3]. Ryan J.W., Speier J.L., J Org. Chem., 1966, 31, 2968-2974.[4]. Hayes R.E., et al, Appl Catal., B, 2000, 25, 93-104.405
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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
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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
Page 353 and 354: PP-II-11COMBINED APPROACH (FMEA- HA
Page 355 and 356: PP-II-12Testing the pilot variant o
Page 357 and 358: PP-II-14NOVEL MICROREACTOR FOR THE
Page 359 and 360: PP-II-15of 1-2.5 lead to a decreasi
Page 361 and 362: PP-II-16stages. Kinetic parameters
Page 363 and 364: PP-II-17whiskers, which assure an a
Page 365 and 366: PP-II-18с m , с cat - density of
Page 367 and 368: PP-II-19decrease. So, the potential
Page 369 and 370: PP-II-20products became a mixture o
Page 371 and 372: PP-II-21A numerical algorithm and s
Page 373 and 374: PP-II-22motions at any external con
Page 375 and 376: PP-II-23One of the main technologic
Page 377 and 378: PP-II-24100 m x 250 μm x 0.5 μm,
Page 379 and 380: PP-II-25A model was developed to ca
Page 381 and 382: PP-II-26The results of calculations
Page 383 and 384: PP-II-27modes of reaction and two d
Page 385 and 386: PP-II-29OZONE-DESTRUCTION REACTOR B
Page 387 and 388: PP-II-30Fig. 1. Axial profile of me
Page 389 and 390: PP-II-31isobutylene in butene fract
Page 391 and 392: PP-II-322.5x10 -3 ( i )2.5x10 -3 (
Page 393 and 394: PP-II-33No olefinreadsorptionWith o
Page 395 and 396: PP-II-34using titania or Ag-doped t
Page 397 and 398: PP-II-35accidents, is condition dep
Page 399 and 400: PP-II-36be seen that at temperature
Page 401 and 402: PP-II-37the solid phase solute conc
Page 403: PP-II-38As shown in Table 1, the ca
Page 407 and 408: PP-II-40Hydrodynamic regime in the
Page 409 and 410: PP-II-41activity, relative unit1,21
Page 411 and 412: PP-II-42One of the major indicators
Page 413 and 414: PP-II-43These conditions are confor
Page 415 and 416: PP-II-44For the hepten, alpha-methy
Page 417 and 418: PP-II-46PARTIAL OXIDATION OF METHAN
Page 419 and 420: PP-II-47DEVELOPMENT OF VORTEX APPAR
Page 421 and 422: MODELING OF CFTALYTIC α-OLEFINS OL
Page 423 and 424: PP-II-49Hinselwood kinetic equation
Page 425 and 426: 3) iterate concentrations at a cut
Page 427 and 428: PP-II-51data such flow sheet provid
Page 429 and 430: PP-II-53ON THE TECNOLOGY OF TECHNIC
Page 431 and 432: PP-II-54PROPYLENE POLYMERIZATION AN
Page 433 and 434: REACTOR FOR LIQUID-PHASE PROCESSES
Page 435 and 436: PP-II-56MODELING OF CATALYTIC MICRO
Page 437 and 438: PP-II-57MATHEMATICAL MODELING OF BE
Page 439 and 440: PP-II-58HONEYCOMB CATALYSTS WITH PO
Page 441 and 442: POSTER PRESENTATIONSSECTION IIISECT
Page 443 and 444: ReferencesPP-III-1[1]. A.N. Pestrya
Page 445 and 446: PP-III-2Table1. Percentages of diff
Page 447 and 448: PP-III-3conversion for the reaction
Page 449 and 450: PP-III-4900Reformer temperature (K)
Page 451 and 452: PP-III-5Catalytic performance of th
Page 453 and 454: 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
Page 605 and 606:
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
Page 619 and 620:
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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