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PP-III-41MODELLING AND DESIGN OF THE REACTORS FOR THE PROCESSOF THERMOCATALYTIC HYDROGENATION OF LIQUIDPRODUCTS OF PYROLYSIS FOR OBTAINING BENZENEA.I. Babaev, A.M. Aliyev, A.Z. TahirovAzerbaijan National Academy of Sciences, Institute of Chemical Problems,e-mail: ITPCHT@itpcht.ab.azAt present, sources of raw material for obtaining of benzene are the aromatichydrocarbons C 7 -C 9 and hydrorefined fraction of pyrocondensate, benzene-tolnenexylene(BTX).Hydrodealkylation and hydrocracking of non-aromatic hydrocarbons of BTXfraction is carried out by thermal and catalytic methods under pressure of hydrogen, 2.5-6.3 MPa and at high temperature, 620-730°C. Shortages of the thermal process are greaterformation of polycyclic aromatic hydrocarbons, lesser yield of ethane and propane and hightemperature. Shortages of the catalytic process are high pressure, complication of regulationof temperature and large expenditure of the catalyst.In our Institute it has been developed the thermocatalytic process which combines theadvantages of thermal and catalytic processes [1]. Thermocatalytic version of the processforesees the realization of hydrogenation of BTX fraction in two consecutive adiabaticreactors. In the first reactor with injection mixing, the degree of hydrocracking achieves 90%.In the second reactor with the polyfunctional catalyst – B-17/3, the reaction of hydrocrackingof non-aromatic hydrocarbons finishes completely. At the description of mechanism of theprocess we have considered the aromatic hydrocarbons, С 8 ; naphthene hydrocarbons, C 6 -C 8 ;paraffin hydrocarbons, C 6 -C 8 and hydrocarbons, C 1 -C 4 in the aggregated form. Taking intoaccount that hydrodynamics of the injection reactor corresponds to model of ideal stirred, thekinetic model of the thermal reactor may be written as:P = P1PP = PPPP23456= P= P= P= PT = T0102030405060+ V+ V+ V+ V+ V+ V⎛+ V ⎜−⎝( R2− R1)/v( R1− 2R5− R6)( − R2)/v( R6− R3)/v( R3− R4)/v( R )/v56∑i=1/ v⎞Ri ΔHi/ CpρRT−αX/⎠( T − T ) ⎟ vwhere R i is a rate of reaction i; ∆H i is a heat of reaction i; C P is an average heat capacity ofthe reaction environment; ρ is a density of the reaction environment; V is a volume of the382(1)
PP-III-41rector; v is a volumetric flow rate; T X is the local wall temperature; α is a heat transferP 1P 20 0 0 0 00coefficient; , , , , and are the initial partial pressure of: toluene, benzene,aromatic hydrocarbons C 8 , naphthene hydrocarbons C 6 -C 8 , paraffin hydrocarbons C 6 -C 8 andcondensation hydrocarbons accordingly.P 3P 4P 5Equations of a rate for i-th reactions:R =RR1.5 0.51k1P1P7where P 7 is partial pressure of hydrogen.P 6R =1.5 0.52k2P3P73= k3P4P7− k7P5R4= k4P5P7235= k5P2− k8P6P7R6 = k5P2P7− k9P4For taking into account of influence of pressure, temperature and ratio of hydrogen to rawmaterial on the rate constants we have used the modified equation of Arrhenius which isgiven byki= Kwhere θ is ratio of hydrogen to raw material.( − ( E + ΔV( P 1)) RT )αi 0iθexpi i− /By using model (1) it has been calculated the construction parameters of the injectionrectors with productivity on raw material 31 ton/h.For calculating of the catalytic reactor it has been used two-dimensional one-phase quasihomogeneonsmodel of the reactor with fixed bed catalyst.Literature1. Далин М.А. и др. Нефтехимические процессы и пути повышения их эффективности. М.,ЦНИИТЭнефтихим, 1981,44 с.383
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Boreskov Institute of Catalysis of
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Mikhail G. Slinko,Honour ChairmanVa
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PLENARY LECTURES
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PL-1built up from an intrinsic cont
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PL-3DEVELOPMENT OF ZEOLITE-COATED M
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PL-4processes in order to evaluate
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PL-5CATALYTIC PARTIAL OXIDATION OF
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KEY-NOTE PRESENTATIONS
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KN-2GETTING TO THE POINT: FROM MOLE
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KN-3PROBLEMS AND PROSPECTS FOR IMRO
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KN-4remain out of the sight of rese
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KN-5SSITKA allows to study not only
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KN-6individual reaction stages with
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Section 1.Kinetics of catalytic rea
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OP-I-1-specialthat Г s /f changed
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OP-I-3-specialKINETIC MODELING OF L
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OP-I-4PARTIAL OXIDATION OF TOLUENE
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OP-I-5Also, the approach to modelin
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OP-I-6starch granules, but after a
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OP-I-8KINETICS OF CARBON MONOXIDE O
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OP-I-9CHAOTIC DYNAMICS IN THE THREE
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OP-I-10ADSORPTION OF COMPLEX MOLECU
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OP-I-11KINETIC ASPECTS OF METHANE O
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OP-I-12KINETIC STUDIES IN STRUCTURE
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OP-I-13A STUDY ON THERMAL COMBUSTIO
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OP-I-14KINETICS OF THE CONVERSION O
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OP-I-15HYDROCRACKING OF LONG CHAIN
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OP-I-16KINETICS IN THE HYDROGENATIO
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OP-I-17MECHANISM OF FORMATION OF ET
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OP-I-18KINETIC STUDIES OF PROPANE D
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OP-I-19ACTIVITY AND DEACTIVATION OF
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OP-I-20GAS PHASE OXIDATION OF FORMA
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OP-I-21Where k A is the rate consta
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OP-I-22al., 2008; Monolith, 2008).
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OP-I-23Fig. 1. Scheme of the FIM ma
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OP-I-24Θ DZ centersdeactivationr D
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OP-I-25equation [2] to nitrogen iso
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OP-II-1CHEMICAL NANOREACTORS AS BAS
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OP-II-2gas model use, there is no n
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OP-II-3Taking into account these pr
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OP-II-4WATER2METH1STEAM2AOFF3AIR10O
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OP-II-5completely dry, at the same
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OP-II-6Many factors have been found
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OP-II-7mechanistic and kinetic stud
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OP-II-9MODELLING OF DIESEL PARTICUL
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Section 3.Catalytic processesí dev
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OP-III-1BIC’s catalyst for N 2 О
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OP-III-2powder sample with the same
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OP-III-3Analysis of the results sho
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OP-III-4Exhaustaftertreatmenttechno
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OP-III-6SOME PROPERTIES OF PEROVSKI
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OP-III-7with the conventional react
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OP-III-8resistance is the membrane
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OP-III-9mass dispersion and to anal
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OP-III-11PROCESS INTENSIFICATION US
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OP-III-12ETHYL ACETATE SYNTHESIS BY
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OP-III-12products are vaporized and
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OP-III-13The reforming reaction was
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OP-III-14reactivity (compared to ot
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OP-III-15Fig. 2. The spent Smopex-1
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OP-III-16Numbers of curves are acco
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OP-III-17perimeter were determined.
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OP-III-18of 2. MSR has been coupled
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OP-III-19chemisorption heat and pro
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OP-III-20In the experiments, total
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OP-III-21obtained by the new techno
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OP-III-22reactor wall from the two-
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OP-III-23and parameters of synthesi
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OP-III-24Results and discussionThe
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OP-IV-1DEEP DESULPHURIZATION OF PET
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OP-IV-2LACTIC ACID AS A BACKGROUND
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OP-IV-3CO REMOVAL FROM H 2 -rich GA
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OP-IV-4REFORMING OF ETHANOL OVER ME
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OP-IV-5MODELING OF HYDROGEN PRODUCT
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OP-IV-6PRODUCTION OF HYDROGEN FROM
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OP-IV-7SYNTHESIS GAS PRODUCTION FRO
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OP-IV-8HYDROGEN PRODUCTION FROM MET
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OP-IV-9A NEW GENERATION OF SUPER-TH
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OP-IV-10EXERGY ANALYSIS OF ENZYMATI
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OP-IV-11ADVANCEMENT OF SLURRY BUBBL
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OP-IV-12Pd-DOPED PEROVSKITE CATALYS
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OP-IV-13HYDROGEN PRODUCTION VIA MET
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Section 5.Catalytic processing of r
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OP-V-1Scheme 1. The developing path
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OP-V-2An example of the model compo
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OP-V-3catalysts were shown to be su
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OP-V-4Catalyst deactivation was mor
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OP-V-53) Study of the FFAs esterifi
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OP-V-6In the present work, a compre
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OP-V-7Ca 2 Fe 2 O 5 , MgFe 2 O 4 an
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OP-V-8cellulose components decompos
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OP-V-9sintering a couple of spirale
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OP-V-10Catalyst preparationA series
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OP-V-11Catalysts characterizationIn
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OP-V-12Kinetic ExperimentsHexadecan
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OP-V-13DESIGN OF PILOT REACTOR AND
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OP-V-14DEVELOPMENT OF A LAB SCALE C
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OP-V-15DEVELOPMENT OF TWO-STAGE PRO
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OP-V-15The data of Table 2 show, th
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OP-V-17ENERGY PRODUCTION FROM BIOMA
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OP-V-18CATALYTIC PARTIAL OXIDATION
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OP-V-19A PHOTOCATALYTIC REACTOR FOR
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OP-V-20BIOMASS GASIFICATION IN A CA
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OP-V-21ESTIMATION OF OPTIMAL REACTO
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POSTER PRESENTATIONSSection 1. Kine
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PP-I-1CONVERSION OF ETHANOL OVER CO
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PP-I-2LATERAL INTERACTIONS, FINITE
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PP-I-3UTILIZATION OF TAFT EQUATION:
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PP-I-4SELECTIVE HYDROGENATION OF CI
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PP-I-5NON OXIDATIVE REGENERATION ME
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PP-I-6Table 1. Parameters in kineti
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PP-I-7where: k nc , k 1 , k a , k b
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PP-I-8After each adsorption or deso
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PP-I-9The increase in pressure, in
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PP-I-10The analysis of the composit
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PP-I-11The network of βP oxidation
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PP-I-12order of magnitude lower. Th
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PP-I-13ab1,01,0Isotope fraction0,5[
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PP-I-14Relations ‘rate vs alcohol
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PP-I-15[EEAA] t , M[EEAA] t -1 , M
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PP-I-17NEW OSCILLATING REACTION:CAR
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PP-I-18NEW OSCILLATING REACTIONS OF
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PP-I-19KINETICS OF GAS-LIQUID PROCE
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PP-I-20COMPLETE OXIDATION OF HARMFU
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PP-I-21THEORETICAL RESEARCH OF SURF
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PP-I-22INFLUENCE OF ORGANIC HELATES
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PP-I-23The equation of the reaction
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PP-I-25SELECTIVE OXIDATION OF METHA
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PP-I-26coefficients of the equation
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PP-I-27into propionic acid. The giv
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PP-I-28In the studied range of temp
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PP-I-29Table. Reaction temperature
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PP-I-30other in both direction of t
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PP-I-31Reynolds number. The boundar
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PP-I-32NANOPARTICLES AND CATALYSISI
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Section 2.Physico-chemical and math
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PP-II-1For investigation, we used n
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PP-II-2criterion «Zn dissolved in
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PP-II-3exist around the steady stat
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PP-II-4in range 0-1. In our case n
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PP-II-5at comparable activity, the
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PP-II-7CFD-CALCULATION OF MALDISTRI
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PP-II-8INVESTIGATION OF NONLINEAR P
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PP-II-8reactivity. There is a small
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PP-II-10CALCULATION OF INDUSTRIAL C
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PP-II-11type of reactors a catalyst
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PP-II-13MATHEMATTICAL MODELLING OF
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PP-II-13where I Э , M 1Э , M 2Э
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PP-II-14where TOC 0 is the initial
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PP-II-16AUTOCATALYTIC REACTION FRON
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Section 3.Catalytic processesí dev
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PP-III-1for the traditional scheme
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PP-III-2Initial conditions: С i (0
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PP-III-3Afterward, a 30% aqueous hy
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PP-III-4The influence of the water
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PP-III-5Vanadium oxide was grafted
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PP-III-6(T p ) was taken as an inde
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PP-III-7dCdτLABdCNABdτdCdτdCdτd
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PP-III-8O 2 , balanced by He, at a
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PP-III-9Solution of system (3) for
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PP-III-10HDT330ºCHDT350ºCHDT370º
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PP-III-11The activity of Au/support
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PP-III-1249775 m 3 /h0,65Initial te
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PP-III-13through one layer of ACC w
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PP-III-14the runs was always higher
Page 332 and 333: PP-III-15The experimental data for
Page 334 and 335: PP-III-16Catalytic hydrogenation of
Page 336 and 337: PP-III-17The following parameters a
Page 338 and 339: PP-III-18Figure 1 - Dependence of t
Page 340 and 341: PP-III-19Our method has some advant
Page 342 and 343: PP-III-20Furthermore, Ayude et al.
Page 344 and 345: PP-III-22OPTIMIZATION OF THE METHAN
Page 346 and 347: PP-III-23EXPERIMENTAL INVESTIGATION
Page 348 and 349: PP-III-24CATALYTIC REACTORS WITH HY
Page 350 and 351: PP-III-25ACTIVITY OF Cu/ZSM-5 CATAL
Page 352 and 353: PP-III-26SIMULATION AND OPTIMISATIO
Page 354 and 355: PP-III-27model of plug flow reactor
Page 356 and 357: PP-III-28Calculations were experime
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Page 360 and 361: PP-III-30adequacy of multistage mod
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Page 364 and 365: PP-III-32procedure presented by Mar
Page 366 and 367: PP-III-33HPA-x + 2 H + + Pd 0 ⎯
Page 368 and 369: PP-III-34of the process as well as
Page 370 and 371: PP-III-35This study was financially
Page 372 and 373: PP-III-36phase. Peroxopolyoxometall
Page 374 and 375: PP-III-37performed under atmospheri
Page 376 and 377: PP-III-38orders of magnitude larger
Page 378 and 379: PP-III-39CATALYTIC REACTORS WITH ST
Page 380 and 381: PP-III-40THE OXIDATIVE DEHYDROGENAT
Page 384 and 385: PP-III-42COMPLEX TECHNOLOGY OF TREA
Page 386 and 387: PP-III-43PHOTO ELECTROCHEMISTRY APP
Page 388 and 389: PP-III-45MODELING OF CATALYTIC α-O
Page 390 and 391: PP-III-46steady states. It was show
Page 392 and 393: PP-III-47Results and discussion:The
Page 394 and 395: PP-III-49FIBROUS PALLADIUM-SUPPORTE
Page 396 and 397: Section 4.Catalytic technologies in
Page 398 and 399: PP-IV-1method is adiabatic or autot
Page 400 and 401: PP-IV-2It had been established that
Page 402 and 403: PP-IV-4INTERACTION OF ACTIVATED ALU
Page 404 and 405: PP-IV-5ENVIRONMENTALLY FRIENDLY PRO
Page 406 and 407: PP-IV-6THE 5%Ni-2%Au/Al 3 CrO 6 SYS
Page 408 and 409: PP-IV-7MESOPOROUS ANODES BASED ON Y
Page 410 and 411: PP-IV-8ADVANCED OXIDATION PROCESS F
Page 412 and 413: PP-IV-9PROCESSING OF POLYMERIC CORD
Page 414 and 415: PP-IV-10EFFECT OF SULPHUR ON THE CA
Page 416 and 417: PP-IV-11OXIDATIVE CONVERSION OF MET
Page 418 and 419: PP-IV-13CATALYTIC FLUE GAS CONDITIO
Page 420 and 421: PP-IV-14RIBBON POROUS NICKEL BASED
Page 422 and 423: PP-IV-15ETHANOL CONVERSION TO HYDRO
Page 424 and 425: PP-IV-16A HIGH-EFFICIENT MICROREACT
Page 426 and 427: PP-IV-17DIRECT DECOMPOSITION OF NIT
Page 428 and 429: PP-IV-18NICKEL CATALYSTS BASED ON P
Page 430 and 431: PP-IV-19SELECTION OF FAVOURABLE FEE
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PP-IV-20FORMALDEHYDE FORMATION DURI
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PP-IV-21PRODUCTION OF HYDROGEN-RICH
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PP-IV-22INFLUENCE OF COMPOSITION OF
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PP-IV-24ONE-STAGE CATALYTIC CONVERS
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PP-IV-25THE STUDY OF METHANE DEHYDR
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PP-IV-26MCM-41-SUPPORTED PdNi CATAL
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PP-IV-27IMPROVING THE FLOW SHEET OF
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PP-IV-29THE PARTIAL OXIDATION OF CH
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PP-IV-30PRODUCTION OF CO-FREE HYDRO
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PP-IV-31PHOTOCATALYTICAL ACTIVITY O
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PP-IV-32NEW ELECTRODE MATERIALSFOR
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PP-IV-33THE CATALYTIC HYDROGENATION
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PP-IV-34W 0, μmol O 2/min0,25 1. 1
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PP-V-1INFLUENCE OF ICE ON MEAs OF P
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PP-V-2DIRECT OILS HYDROGENATION TO
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PP-V-3DEVELOPMENT OF Pd/SIBUNIT CAT
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PP-V-4Pt NANOPARTICLE-HOLLOW POROUS
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PP-V-5THE PROCESS FOR PRODUCING ORG
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PP-V-6water removing. This method p
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PP-V-7ResultsThe presented technolo
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PP-V-8the most effective catalysts.
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PP-V-9Neither the low sulphur conte
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PP-V-10composition (methyl esters,
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PP-V-11reactor we can see that its
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PP-V-12Recent studies lead in this
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PP-V-13catalysts (e.g. Pt or Pd), t
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PP-V-14Alkali catalyst. For a basic
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PP-V-15obtaining the related profil
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PP-V-16reaction parameters, not rep
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PP-V-18STUDY OF THE CATALYTIC ACTIV
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PP-V-19BIOMORPHIC CATALYSTS ON THE
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PP-V-20Al,Cu-PILLARED CLAYS AS CATA
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PP-V-21KINETICS OF THE HYDROXYMATAI
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PP-V-22THE NEW METHOD OF OBTAINING
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PP-V-23containing mono- and di-subs
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AUTOCLAVE ENGINEERS COMPANYSYSTEMAT
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CATACON CATACON CATACON CATACON CAT
Page 506 and 507:
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Page 510 and 511:
George AvgouropoulosFoundation for
Page 512 and 513:
Leonid BykovJSC «Chemphyst-Alloy L
Page 514 and 515:
Debora FinoPolitecnico di TorinoCor
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Jenő HancsókUniversity of Pannoni
Page 518 and 519:
Andrey KhudoshinLomonosov Moscow St
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Cristian LedesmaEnergetic Technique
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Uri Matatov-MeytalDepartment of Che
Page 524 and 525:
Karina OjedaIndustrial University o
Page 526 and 527:
Yuri PyatnitskyPisarzhevsky Institu
Page 528 and 529:
Vera ScmachkovaBoreskov Institute o
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Peter StrizhakPisarzhevsky Institut
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Nadezhda VernikovskayaBoreskov Inst
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Nataliya ZubritskayaRSC «Applied C
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ORAL PRESENTATIONS.................
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OP-I-21Saeedizad M., Sahebdelfar S.
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OP-III-9Nekhamkina O., Sheintuch M.
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OP-IV-5Hernández L., Kafarov V.V.M
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OP-V-13Sadykov V., Mezentseva N., V
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PP-I-15PP-I-16PP-I-17PP-I-18PP-I-19
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PP-II-9 Nikiforov A., Paek U-Hyon,
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PP-III-17 Vernikovskaya N.V., Kashk
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PP-III-42 Goshu Y.W., Tsaryov Y.V.,
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PP-IV-17 Ohnishi C.H., Yoshino H.,
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PP-V-9 Hancsók J., Magyar S., Kall
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XVIII International Conference on C
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