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OP-III-B-8TWO STEP PROCESS OF OBTAINING LOW BENZENECONTAINING FUELS FROM ETHANOLMakarfi Y.I. 1 , Tretyakov V.F. 1,2 , Frantsuzova N.A. 1 , Tretyakov K.V. 21 Lomonosov Moscow State Academy of Fine Chemical Technology,119571 Moscow, Russia2 A.V. Topchiev Institute of Petrochemical Synthesis, Moscow, Russiayusufisa@yahoo.comRecent reports have shown that a lot of progress is being made in utilizingethanol obtained from biomass as a fuel in internal combustion engines. However,this advancement is dampened by the need to redesign engines that will easily utilizeethanol without having to blend it. Among the advantages of ethanol over fossil fuel isthe reduction in net emission of carbon dioxide. At the same time among itsshortcomings is the fact that crude oil does not only supply fuels but also a widerange of hydrocarbons through primary and secondary treatment of the raw crude.A more convenient way of fully substituting crude oil with ethanol should ensurethat products obtainable from crude oil can be produced from ethanol. To this effect,much work has been done in converting the liquid obtained from biomass into a widerange of hydrocarbons. As reported in [1], based on reaction conditions, varioushydrocarbons can be obtained by passing ethanol over modified zeolite catalysts.However, It has been observed that the concentration of certain aromatic compoundsin the conversion product is relatively high compared to modern day acceptablestandards in transport fuels (less than 1%). Taking this into consideration, We havedeveloped an effective way of hydrogenating the liquid obtained from ethanolconversion using nano-structured Pt-Rd catalyst. The concentration of aromatichydrocarbons in the upgraded liquid reduces by 50%, with practically no benzene.(Table1.) This makes it possible to produce transport fuels with aromatic content 12-35 %mass. (diagram1). The research shows that ethanol is capable of substitutingcrude oil not only as a source of transport fuel, but as a raw material for otherpetrochemicals.194
OP-III-B-8Table 1.Material balance for 1 tonne of liquid obtained from ethanol conversion.CompoundInputOutputт % mass т % massC 1 -C 4 0.09 7.20 0.10 8.13C 5-9 0.20 16.00 0.88 70.79Benzene 0.02 1.60 0.00 0.01Toluene 0.18 14.40 0.00 0.00Ethylbenzene 0.04 3.20 0.00 0.36m,p, Xylenes 0.25 20.00 0.01 0.63Orto xylenes 0.14 11.20 0.03 2.44Ethylmethyl benzene 0.08 6.40 0.08 6.15Other aromatichydrocarbons 0.00 0.00 0.11 9.05Hydrogen 0.25 20.00 ~ ~Coke +loss - - 0.03 2.44Total 1.25 100 1.25 1005OLEFINSHYDROGEN13810469т112712HYDROCARBONPRODUCTDiagram 1. SETUP FOR OBTAINING TRANSPORT FUELS FROM ETHANOL1 – Bio-ethanol tank, 2 - Pump 3 – Heat exchanger, 4 – Conversion reactor, 5 - Condenser,6 -separator, 7-Pump, 8-Separator, 9-Water tank, 10 – Hydrogenation reactor, 11 – Filter,12-product tank.References[1]. Y.I.Makarfi et al. Conversion of Bio-ethanol over zeolites; Chemical Engineering Journal; 2009;V.154 №-3 – pp 396-400195
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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
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
Page 179 and 180: ORAL PRESENTATIONSSECTION IIIChemic
Page 181 and 182: OP-III-B-1Reactor parameters:Intern
Page 183 and 184: OP-III-B-2JOINT STEAM REFORMING OF
Page 185 and 186: OP-III-B-3LANDFILL BIOGAS PURIFICAT
Page 187 and 188: OP-III-B-4MODELING AND SIMULATION O
Page 189 and 190: OP-III-B-5DemonstratorThe medium-te
Page 191 and 192: OP-III-B-630/19.6 Nl/min (space vel
Page 193: OP-III-B-7mixed in the ratios: 94,8
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
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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
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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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