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PP-I-32IntroductionPROCESS DESIGN OF CO 2 RECOVERY: TECHNICAL,ENVIRONMENTAL AND ECONOMIC EVALUATIONLuis P., Albo J., Garea A., Irabien A.Department of Chemical Engineering and Inorganic Chemistry,University of Cantabria, Avda. Los Castros s/n 39005, SpainFax: +34 942 201591; E-mail: luisp@unican.esCarbon dioxide (CO 2 ) is one of the major contributors to the greenhouse effect.The power and industrial sectors combined account for about 60% of the global CO 2emissions [1] and their recovery is a key issue to guarantee the sustainability ofindustrial processes. Non-dispersive absorption based on membranes hasdemonstrated to be a suitable and technology for gas recovery [2-6] due to itswidespread advantages: controlled interfacial area, independent control of gas andliquid flow rates and it avoids solvent losses due to drops dragging [7, 8]. However,its industrial application is limited by economic considerations that are restricted byenvironmental targets.In this paper, a steady state model is developed to describe the mass transfer ofCO 2 in a polypropylene hollow fibre module (Liqui-Cel, United States). The modeldescribes the mass transfer in the gas and liquid phases and the correspondingdimensionless equations for both phases have been solved simultaneously. It allowsstudying the technical viability, in terms of the influence that operating conditions (gasand liquid flow rates) and solvent affinity (H) have on the process efficiency, and also,the economic and environmental limitations can be evaluated in order to determinethe range of application of the contactor to fulfil a specific target of CO 2 recovery.References[1]. Intergovernmental Panel on Climate Change (IPCC). IPCC special report on carbon dioxidecapture and storage. Cambridge University Press (2005).[2]. Luis P, Ortiz I, Aldaco R, Garea A, Irabien A. Recovery of sulfur dioxide using non-dispersiveabsorption. Int J Chem React Eng 5: art. no. A52 (2007).[3]. Yan S, Fang M, Zhang W, Wang S, Xu Z, Luo Z, Cen K. Experimental study on the separation ofCO 2 from flue gas using hollow fiber membrane contactors without wetting. Fuel Process Technol88 (5): 501 – 511 (2007).[4]. Luis P, Garea A, Irabien A. Sulfur dioxide non-dispersive absorption in N,N-dimethylaniline usinga ceramic membrane contactor, J Chem Tech Biotechnol, 83 (11) 1570 – 1577 (2008).[5]. Katja S, Nijmeijer K, Wessling M. Gas-Liquid membrane contactors for CO 2 removal. J MembraneSci, 340, 214–220 (2009).[6]. Luis P, Garea A, Irabien A. Zero solvent emission process for sulfur dioxide recovery using amembrane contactor and ionic liquids, J Membrane Sci, 330 (1 – 2) 80 – 89 (2009).278
PP-I-32[7]. Karoor S, Sirkar K. Gas Absorption Studies in Microporous Hollow Fiber Membrane Modules. IndEng Chem Res 32 (4): 674 – 684 (1993).[8]. Gabelman A, Hwang S. Hollow fiber membrane contactors. J Membrane Sci 159 (1-2): 61 – 106(1999).AcknowledgmentsThis research is financially supported by the Spanish Ministry of Science and Technology (ProjectCTM2006-00317).279
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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
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
Page 245 and 246: PP-I-14THE INVESTIGATION OF REACTIO
Page 247 and 248: PP-I-15The qualitative picture of s
Page 249 and 250: Thus, knowing the composition of ra
Page 251 and 252: PP-I-17current density. Preliminary
Page 253 and 254: PP-I-18Hydrogenation kinetics was d
Page 255 and 256: PP-I-19the active mixing, amplitude
Page 257 and 258: PP-I-20where r, h indicate the radi
Page 259 and 260: PP-I-21model is very anisotropic be
Page 261 and 262: PP-I-22- Reduction of the number of
Page 263 and 264: PP-I-23oscillations of intermediate
Page 265 and 266: PP-I-25SYNTHESIS OF ETHYLENE OXIDE
Page 267 and 268: PP-I-26OPTIMUM KINETICS FOR POLYSTY
Page 269 and 270: PP-I-27TableSpecific surface area (
Page 271 and 272: PP-I-28γ-preirradiated sample), th
Page 273 and 274: PP-I-29commercial CFD solver FLUENT
Page 275 and 276: PP-I-30modulus, a considerable decr
Page 277: PP-I-31The destruction ways of CF 3
Page 281 and 282: PP-I-33above 750°. The catalytic p
Page 283 and 284: PP-I-35REVERSE FLOW REACTOR WITH FO
Page 285 and 286: FLOW-RECIRCULATION METHOD FOR INVES
Page 287 and 288: TO A PROBLEM OF OPTIMIZATION OF FUN
Page 289 and 290: PP-I-38THE INFLUENCE OF REACTION MI
Page 291 and 292: PP-I-39METHANOL OXIDATIVE STEAM REF
Page 293 and 294: PP-I-41CORRECT INVESTIGATION OF THE
Page 295 and 296: PP-I-42NEW APPROACH OF DEFINITION O
Page 297 and 298: PP-I-43STREAM HEAT EXCHANGE OF AERO
Page 299 and 300: PP-I-44HIGH TEMPERATURE OXYGEN TRAN
Page 301 and 302: PP-I-45KINETICS OF TRANSESTERIFICAT
Page 303 and 304: MATHEMATICAL MODELING AND OPTIMIZAT
Page 305 and 306: PP-I-47The basic side reaction is r
Page 307 and 308: PP-I-49EXPERIMENTAL STUDY OF THE HA
Page 309 and 310: PP-I-51ON THE KINETICS AND REGULARI
Page 311 and 312: PP-I-52DIFFERENTIAL THERMAL ANALYSI
Page 313 and 314: PP-I-53oxidation reaction demonstra
Page 315 and 316: PP-I-54of reaction. It is establish
Page 317 and 318: PP-I-55effects, are energetically c
Page 319 and 320: PP-I-56The experiments and simulati
Page 321 and 322: PP-I-57In the studied range of temp
Page 323 and 324: PP-I-58HeadingsAdvances in Chemical
Page 325 and 326: PP-I-59calculated. During the aroma
Page 327 and 328: 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
Page 533 and 534:
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
Page 555 and 556:
THREE-PHASE DIRECT OILS HYDROGENATI
Page 557 and 558:
Co-BASED CATALYSTS FOR THE HYDROLYS
Page 559 and 560:
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
Page 565 and 566:
PP-III-68INFLUENCE OF SPILLOVER ON
Page 567 and 568:
PP-III-69AEROBIC OXIDATIVE COUPLING
Page 569 and 570:
PP-III-70MECHANISMS FOR CHEMICAL RE
Page 571 and 572:
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
Page 579 and 580:
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
Page 597 and 598:
ARKHIPOV Vladimir AfanasievichResea
Page 599 and 600:
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
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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
Page 615 and 616:
SULMAN Esfir MikhailovnaTver Techni
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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
Page 623 and 624:
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
Page 631 and 632:
PP-II-45 Stepanek J., Koci P., Kubi
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PP-III-19 Fedorova Z.A., Danilova M
Page 635 and 636:
PP-III-53 Pölczmann G., Valyon J.,
Page 637:
XIX International Conference on Che
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