Boreskov Institute of Catalysis SB RAS, Novosibirsk, Russia

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PP-59KINETICS OF CATALYTIC GASIFICATION OF LIGNITE WITHCARBON DIOXIDE BY THERMOGRAVIMETRYVergel Bungay 1 , Byungho Song 1 , Sangdone Kim 2 , Jungmin Sohn 3 ,Yongjeon Kim 4 , Gyootae Kim 4 , Sam R. Park 41 Chemical Engineering Department, Kunsan National University, Gunsan,Jeonbuk 573-701, Korea, bungayvc@live.com; bhsong@kunsan.ac.kr2 Department of Chemical and Biomolecular Eng., KAIST, Daejeon 305-701, KoreaKimsd45@kaist.ac.kr3 Department of Mineral Resources & Energy Eng., Chonbuk National University,Jeonju, Jeonbuk 561-756, Korea, jmsohn@jbnu.ac.kr4 SK Energy Institute of Technology, Daejeon 305-712, Koreayjkimej@skenergy.com; gtkim@skenergy.com; srpark@skenergy.comThe catalytic effect on the gasification rate of lignite with CO 2 was determined bythe thermogravimetric method. The tested catalytic single salts are K 2 CO 3 , Na 2 CO 3 ,K 2 SO 4 and FeSO 4 . The gasification experiments were carried out by using lignitecoal loaded with 5-15% catalyst at temperature ranging from 600°C to 900°C andambient pressure with N 2 -CO 2 reactant gas mixture. The kinetic parameters weredetermined by the modified volumetric reaction model. Potassium carbonate exhibitsthe highest catalytic activity at the given temperature and catalyst loading. It wasobserved that complete carbon conversion was obtained within 10 min with thecatalyst at 800°C in the following catalytic activity as K 2 CO 3 > Na 2 CO 3 > K 2 SO 4 >FeSO 4 . Enhancement of the gasification rate is found to ranged from 1.5-18 timesthat of the uncatalyzed reaction. Activation energy of the gasification with K 2 CO 3 ,Na 2 CO 3 , K 2 SO 4 , and FeSO 4 are found to be 124.9, 134.6, 201.9, and 155.0 kJ/mol,respectively, as within the range reported in the literature [1-3]. The apparent reactionrate of catalytic coal gasification is proposed for each catalyst.References:[1]. Carbon 1984, Vol. 22, pp. 173-176.[2]. Fuel 1993, Vol. 72, pp. 797-803.[3]. Fuel Process. Technol. 2008, Vol. 89, pp. 890-896.Acknowledgements:This work was supported by Energy Efficiency and Resources R&D program(2009T100100675) under the Ministry of Knowledge Economy, Republic of Korea.150
PP-60EFFECT OF RESIDENCE TIME OF THE ACIDIC AND BASICHYDROLYSIS OF THE SUGARCANE BAGASSE ON THEFEEDSTOCK AND PYROLYSIS DERIVATIVE BIO-OIL PROFILESMatheus O. Souza 1 , Marcelo M. Pereira 1 , Margareth Rose L. Santos 1 ,Luciana T. Santos 2 , Josilaine A. Cunha 1 and Ligia M. M. Valente 11 Federal University of Rio de Janeiro, CT, bloco A, 7º andar, RJ, CEP 21941-909,Brazil, FAX 55-21-2562-7240, m.oliveira13@ig.com.br2 Nacional Agency of Petroleum, Av. Rio Branco, 65, RJ, BrazilThe use of agricultural residues as a potential resource of renewable energy hasbeen worldwide investigated and it seems to be very attractive and opportune toutilize sugarcane bagasse for the Brazilian energy needs. This work reports theinfluence of the residence time of the acidic and alkaline pretreatment of sugarcanebagasse on the biomass feedstock and on the Low Temperature Conversion (LTC)pyrolysis derivative bio-oil profiles. Hydrolyses were carried out at 120°C in acidic(HCl 2M) and basic (NaOH 2M) moiety by 1, 3 and 5 h. Both non- and pretreatedbiomasses were analyzed by FTIR. The LTC-pyrolysis experiments were performedin a home-made «U» type glass reactor apparatus under N 2 atm at 20-120°C(5°C/min rate), 120-350°C (10°C/min) and then 350°C by 15 min. The liquid fraction,condensed at the reactor outlet, was extracted with acetone. The solvent wasremoved at low pressure and the oily residue was analyzed by 1 H NMR at 200 MHzin acetone-d 6 . The comparative FTIR feedstock spectra profiles of the hydrolyzedand non-hydrolyzed bagasses showed, independent of the time of reaction, a strongdecrease in the lignin and hemicellulose content for the alkaline hydrolyzed bagasseand just a significant decrease on the hemicellulose content for the acidic hydrolyzedbagasse. The comparative 1 H NMR bio-oil spectra profiles showed through thecorrelation among the peak areas at 3-5 ppm (carbohydrates) and those at 9-10 ppm(furfurals) plus those at 6-8 ppm (phenylics+furfurals) an increase of carbohydratecontent after acidic hydrolysis, independent of the reaction time, and themaintenance of the carbohydrate content with a discrete increment along theincrease of the reaction time after the basic hydrolysis. Thus it can be concluded thatthe hydrolysis pretreatment, independent of the resident time, affect the compositionof both sugarcane bagasse and its pyrolosis bio-oil derivative profiles. In addition theyield % of the bio-oil obtained from the acidic hydrolyzed bagasse was 2.4 timesgreater than those obtained from the basic hydrolyzed bagasse.Acknowledgement. PETROBRAS for financial support.151
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Boreskov Institute of Catalysis SB
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International Scientific CommitteeV
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PL-1DESIGN OF CATALYSTS AND CATALYT
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PL-3CATALYTIC TRANSFORMATIONS FOR P
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PL-4In this contribution the princi
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PL-5THEORETICAL AND EXPERIMENTAL AN
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PL-6heat exchanging internals; dyna
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CATALYTIC CRACKING OF SUNFLOWER SEE
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KN-3CONVERSIONS OF WOOD AND CELLULO
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CATALYTIC FUEL-GAS CLEANING IN A ST
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BIO4ENERGY - THE SWEDISH QUESTFOR S
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ORAL PRESENTATIONSSection 1.CATALYS
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OP-1-2METHANOLYSIS OF VEGETABLE OIL
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OP-1-4SYNTHESIS, CHARACTERIZATION A
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OP-1-6THE PRODUCTION OF MOTOR FUEL
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HYDROTREATMENT CATALYSTS DESIGN FOR
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CATALYTIC HYDROTREATING OF FAST PYR
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OP-1-11BIOMASS’ PRODUCTS TREATMEN
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OP-1-14BIO-ETHANOL - PETROCHEMICAL
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OP-1-15USING BIOMASS-BASED FUELS FO
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OP-2-1COMBINATION OF METAL AND ACID
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OP-2-3CELLULOSE HYDROTHERMAL CONVER
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OP-2-4CATALYTIC CONVERSION OF CONCE
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OP-2-6KINETICS OF SELECTIVE OXIDATI
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OP-2-8PROCESS FOR THE PRODUCTION OF
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OP-2-10BIODERIVED LACTIC ACID AND L
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OP-2-11CATALYTIC CONVERSION OF HEMI
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OP-2-13Cu CATALYSTS FOR HYDROGENOLY
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OP-2-15Cu-CONTAINING CATALYSTS FOR
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OP-2-16MICROWAVE-ASSISTED EPOXIDATI
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OP-2-18ULTRASOUND-INDUCED FORMATION
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OP-2-20EFFECT OF Ag DOPING IN La-Mn
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OP-2-22INSIGHTS IN GLYCEROL REFORMI
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OP-3-1APPLICATION OF NOVEL CATALYST
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OP-3-2REDUCING CONVERSIONS OF GLYCE
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OP-3-4LOW-TEMPERATURE CONVERSION OF
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OP-3-6H 2 PRODUCTION BY STEAM REFOR
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OP-3-8CATALYTIC STEAM REFORMING OF
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OP-3-10CATALYTIC GAS PHASE CONVERSI
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ORAL PRESENTATIONSSection 4.BIOCATA
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OP-4-2THE EFFECT OF OXYGEN MASS TRA
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OP-4-4VALORIFICATION OF FERMENTATIO
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OP-4-5MECHANISM OF ULTRASOUND-ASSIS
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PP-1THE ORTHO - PARA CONVERSION OF
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PP-3THREE-STAGE WASTE-FREE PROCESS
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PP-4Н 2 О with formation superflu
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PP-6HYDROGEN FROM FORMIC ACID DECOM
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PP-8VALORIZATION OF GLYCEROL BY CON
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PP-10BIODIESEL PRODUCTION FROM WAST
Page 100 and 101: PP-11Figure 1. CHEMPAK architecture
Page 102 and 103: PP-13HYDROCONVERSION OF VEGETABLE O
Page 104 and 105: PP-15CaO AND Al 2 O 3 SUPPORT SOLID
Page 106 and 107: PP-17CATALYTIC CRACKING OF GLUCOSE
Page 108 and 109: PP-19[DBU][Ac]: A TASK-SPECIFIC ION
Page 110 and 111: PP-21SELECTIVE CONVERSION OF CARBON
Page 112 and 113: PP-23HYDROGEN PRODUCTION BY ETHANOL
Page 114 and 115: PP-25SUB- AND SUPERCRITICAL WATER A
Page 116 and 117: PP-27THE BLENDING OF SECOND - GENER
Page 118 and 119: PP-29STUDY ON THE PRETREATMENTS OF
Page 120 and 121: PP-31THERMAL CONVERSIONS OF WOOD SA
Page 122 and 123: PP-33PHYSICOCHEMICAL PROPERTIES OF
Page 124 and 125: PP-35LOW-TEMPERATURE OXIDATION OF O
Page 126 and 127: PP-37LABORATORY EQUIPMENT FOR THE S
Page 128 and 129: PP-39FERMENTATION PROCESSES OF FREE
Page 130 and 131: PP-41THERMOCATALYTIC HYDROLYSIS AND
Page 132 and 133: PP-43OBTAINING OF SYNTHETIC FUEL FR
Page 134 and 135: PP-44hydrogen. The highest values o
Page 136 and 137: PP-46PROBLEM OF RECEPTION OF ANTIMA
Page 138 and 139: PP-48INVESTIGATION OF NEW WAYS OF B
Page 140 and 141: PP-50DEVELOPMENT OF AN EFFICIENT ME
Page 142 and 143: PP-52ZEOLITE COATINGS ON SUGAR CANE
Page 144 and 145: PP-54PREPARATION OF ADVANCED ADSORB
Page 146 and 147: PP-56HYDROGENATION OF CIS-METHYL OL
Page 148 and 149: PP-57CAVITATION ASSISTED DESIGH OF
Page 152 and 153: PP-61ORGANOSOLV LIGNIN AS CHEMICALS
Page 154 and 155: PP-62which were taken in preset qua
Page 156 and 157: PP-64EXTRACTION OF HUMIC ACIDS FROM
Page 158 and 159: PP-66THE INVESTIGATION OF ASPECTS O
Page 160 and 161: LIST OF PARTICIPANTSNeisiani ABDOLL
Page 162 and 163: Andrey CHISTYAKOVA.V. Topchiev Inst
Page 164 and 165: Yusuf ISA MAKARFIM.V. Lomonosov Mos
Page 166 and 167: Nikolaj LAPINInstitute of Microelec
Page 168 and 169: Vitaly ORDOMSKYDepartment of Chemis
Page 170 and 171: Irina SIMAKOVABoreskov Institute of
Page 172 and 173: Elena VIALICHPerm State UniversityB
Page 174 and 175: ORAL PRESENTATIONS.................
Page 176 and 177: OP-2-18 Andreeva D., Schäferhans J
Page 178 and 179: PP-15 Dias A.P., Puna J.F., Gomes J
Page 180 and 181: PP-50Rustamov M.I., Abad-zade Kh.I.
Page 182: INTERNATIONAL CONFERENCECATALYSIS F
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Boreskov Institute of Catalysis SB RAS, Novosibirsk, Russia

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