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In Kyu Song - One of the best experts on this subject based on the ideXlab platform.
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catalytic cracking of c5 Raffinate to light olefins over lanthanum containing phosphorous modified porous zsm 5 effect of lanthanum content
Fuel Processing Technology, 2013Co-Authors: Joongwon Lee, Ung Gi Hong, Sunhwan Hwang, Min Hye Youn, In Kyu SongAbstract:Abstract Lanthanum-containing phosphorous-modified porous ZSM-5 catalysts (LaX-P/C-ZSM5) were prepared with a variation of La/Al atomic ratio (X = 0.3, 0.7, 0.9, and 1.2) for use in the production of light olefins (ethylene and propylene) through catalytic cracking of C 5 Raffinate. The effect of lanthanum content of LaX-P/C-ZSM5 catalysts on their physicochemical properties and catalytic activities for the cracking of C 5 Raffinate was investigated. It was found that acidity of LaX-P/C-ZSM5 catalysts decreased with increasing lanthanum content, while basicity of LaX-P/C-ZSM5 catalysts increased with increasing lanthanum content. In the catalytic cracking of C 5 Raffinate, acid and base properties of LaX-P/C-ZSM5 catalysts were closely related to the conversion of C 5 Raffinate and selectivity for light olefins, respectively. Conversion of C 5 Raffinate decreased with decreasing acidity of the catalyst and selectivity for light olefins increased with increasing basicity of the catalyst. Among the catalysts tested, La0.7-P/C-ZSM5 catalyst with moderate acidity and basicity exhibited the best catalytic performance in terms of yield for light olefins. It is concluded that an optimal lanthanum content of LaX-P/C-ZSM5 catalysts was required for maximum light olefin production in the catalytic cracking of C 5 Raffinate.
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production of light olefins through catalytic cracking of c5 Raffinate over carbon templated zsm 5
Fuel Processing Technology, 2013Co-Authors: Joongwon Lee, Ung Gi Hong, Sunhwan Hwang, Min Hye Youn, In Kyu SongAbstract:Abstract ZSM-5 catalysts (C(X)-ZSM-5) with micropores and mesopores were prepared by a carbon templating method with a variation of carbon template content (X = 0, 10, 20, 30, 40, and 50 wt.%), and they were applied to the production of light olefins (ethylene and propylene) through catalytic cracking of C 5 Raffinate. The effect of carbon template content on the physicochemical properties and catalytic activity of C(X)-ZSM-5 catalysts was investigated. It was revealed that physicochemical properties of C(X)-ZSM-5 catalysts were strongly influenced by carbon template content. Adsorption ability for n-pentane and mesopore volume of C(X)-ZSM-5 catalysts increased with increasing carbon template content. It was also found that catalytic performance of C(X)-ZSM-5 catalysts was closely related to the mesoporosity of the catalyst. Conversion of C 5 Raffinate and yield for light olefins increased with increasing mesopore/micropore volume ratio of the catalyst, while selectivity for ethylene and propylene showed constant values. Thus, carbon template content in the C(X)-ZSM-5 catalysts strongly affected the mesoporosity of the catalyst, and in turn, mesoporosity played an important role in determining the catalytic performance in the production of light olefins through catalytic cracking of C 5 Raffinate.
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a synergistic effect of α bi2mo3o12 and γ bi2moo6 catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Journal of Molecular Catalysis A-chemical, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, Howon Lee, In Kyu SongAbstract:Abstract α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were prepared by a co-precipitation method for use in the oxidative dehydrogenation of C 4 Raffinate-3 to 1,3-butadiene. A series of mixed catalysts composed of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 were also prepared by a mechanical mixing method to investigate any synergistic effects of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3. The α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were formed successfully, as confirmed by XRD, FT-IR, Raman spectroscopy, and ICP-AES analyses. The γ-Bi 2 MoO 6 catalyst exhibited a better catalytic performance than the α-Bi 2 Mo 3 O 12 catalyst due to its facile oxygen mobility. The conversion of n-butene and the yield for 1,3-butadine over the mixed catalysts showed volcano-shaped curves with respect to γ-Bi 2 MoO 6 content due to the synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts. Among the mixed catalysts, the catalyst composed of 10 wt.% α-Bi 2 Mo 3 O 12 and 90 wt.% γ-Bi 2 MoO 6 showed the best catalytic performance. The γ-Bi 2 MoO 6 catalyst retained a higher oxygen mobility than the α-Bi 2 Mo 3 O 12 catalyst, while the α-Bi 2 Mo 3 O 12 catalyst retained much more adsorption sites for n -butene than the γ-Bi 2 MoO 6 catalyst. The synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3 was due to a combination of the facile oxygen mobility of γ-Bi 2 MoO 6 and the abundant adsorption sites of α-Bi 2 Mo 3 O 12 for n -butene.
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catalytic performance of bismuth molybdate catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Applied Catalysis A-general, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, In Kyu SongAbstract:Abstract α-Bi2Mo3O12 and γ-Bi2MoO6 were prepared by a co-precipitation method, and were applied to the oxidative dehydrogenation of C4 Raffinate-3 to 1,3-butadiene. Both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts were thermally and structurally stable during the catalytic reaction. They exhibited a stable catalytic performance in the oxidative dehydrogenation of C4 Raffinate-3 without catalyst deactivation. However, the catalytic performance of γ-Bi2MoO6 was superior to α-Bi2Mo3O12 due to the facile oxygen mobility of γ-Bi2MoO6. The reactivity of n-butene isomers in the C4 Raffinate-3 decreased in the order of 1-butene > trans-2-butene > cis-2-butene over both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts. Steam played an essential role in suppressing CO2 formation, and furthermore, served as a heat sink for preventing hot spots or reactor run-away. In the catalytic reaction with respect to reaction temperature, the maximum conversion of n-butene (ca. 66%) and the maximum yield for 1,3-butadiene (ca. 60%) were achieved at 440 °C over the γ-Bi2MoO6 catalyst (n-butene:oxygen:steam = 1:0.75:15).
Ji Chul Jung - One of the best experts on this subject based on the ideXlab platform.
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a synergistic effect of α bi2mo3o12 and γ bi2moo6 catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Journal of Molecular Catalysis A-chemical, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, Howon Lee, In Kyu SongAbstract:Abstract α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were prepared by a co-precipitation method for use in the oxidative dehydrogenation of C 4 Raffinate-3 to 1,3-butadiene. A series of mixed catalysts composed of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 were also prepared by a mechanical mixing method to investigate any synergistic effects of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3. The α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were formed successfully, as confirmed by XRD, FT-IR, Raman spectroscopy, and ICP-AES analyses. The γ-Bi 2 MoO 6 catalyst exhibited a better catalytic performance than the α-Bi 2 Mo 3 O 12 catalyst due to its facile oxygen mobility. The conversion of n-butene and the yield for 1,3-butadine over the mixed catalysts showed volcano-shaped curves with respect to γ-Bi 2 MoO 6 content due to the synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts. Among the mixed catalysts, the catalyst composed of 10 wt.% α-Bi 2 Mo 3 O 12 and 90 wt.% γ-Bi 2 MoO 6 showed the best catalytic performance. The γ-Bi 2 MoO 6 catalyst retained a higher oxygen mobility than the α-Bi 2 Mo 3 O 12 catalyst, while the α-Bi 2 Mo 3 O 12 catalyst retained much more adsorption sites for n -butene than the γ-Bi 2 MoO 6 catalyst. The synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3 was due to a combination of the facile oxygen mobility of γ-Bi 2 MoO 6 and the abundant adsorption sites of α-Bi 2 Mo 3 O 12 for n -butene.
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catalytic performance of bismuth molybdate catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Applied Catalysis A-general, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, In Kyu SongAbstract:Abstract α-Bi2Mo3O12 and γ-Bi2MoO6 were prepared by a co-precipitation method, and were applied to the oxidative dehydrogenation of C4 Raffinate-3 to 1,3-butadiene. Both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts were thermally and structurally stable during the catalytic reaction. They exhibited a stable catalytic performance in the oxidative dehydrogenation of C4 Raffinate-3 without catalyst deactivation. However, the catalytic performance of γ-Bi2MoO6 was superior to α-Bi2Mo3O12 due to the facile oxygen mobility of γ-Bi2MoO6. The reactivity of n-butene isomers in the C4 Raffinate-3 decreased in the order of 1-butene > trans-2-butene > cis-2-butene over both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts. Steam played an essential role in suppressing CO2 formation, and furthermore, served as a heat sink for preventing hot spots or reactor run-away. In the catalytic reaction with respect to reaction temperature, the maximum conversion of n-butene (ca. 66%) and the maximum yield for 1,3-butadiene (ca. 60%) were achieved at 440 °C over the γ-Bi2MoO6 catalyst (n-butene:oxygen:steam = 1:0.75:15).
Joongwon Lee - One of the best experts on this subject based on the ideXlab platform.
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catalytic cracking of c5 Raffinate to light olefins over lanthanum containing phosphorous modified porous zsm 5 effect of lanthanum content
Fuel Processing Technology, 2013Co-Authors: Joongwon Lee, Ung Gi Hong, Sunhwan Hwang, Min Hye Youn, In Kyu SongAbstract:Abstract Lanthanum-containing phosphorous-modified porous ZSM-5 catalysts (LaX-P/C-ZSM5) were prepared with a variation of La/Al atomic ratio (X = 0.3, 0.7, 0.9, and 1.2) for use in the production of light olefins (ethylene and propylene) through catalytic cracking of C 5 Raffinate. The effect of lanthanum content of LaX-P/C-ZSM5 catalysts on their physicochemical properties and catalytic activities for the cracking of C 5 Raffinate was investigated. It was found that acidity of LaX-P/C-ZSM5 catalysts decreased with increasing lanthanum content, while basicity of LaX-P/C-ZSM5 catalysts increased with increasing lanthanum content. In the catalytic cracking of C 5 Raffinate, acid and base properties of LaX-P/C-ZSM5 catalysts were closely related to the conversion of C 5 Raffinate and selectivity for light olefins, respectively. Conversion of C 5 Raffinate decreased with decreasing acidity of the catalyst and selectivity for light olefins increased with increasing basicity of the catalyst. Among the catalysts tested, La0.7-P/C-ZSM5 catalyst with moderate acidity and basicity exhibited the best catalytic performance in terms of yield for light olefins. It is concluded that an optimal lanthanum content of LaX-P/C-ZSM5 catalysts was required for maximum light olefin production in the catalytic cracking of C 5 Raffinate.
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production of light olefins through catalytic cracking of c5 Raffinate over carbon templated zsm 5
Fuel Processing Technology, 2013Co-Authors: Joongwon Lee, Ung Gi Hong, Sunhwan Hwang, Min Hye Youn, In Kyu SongAbstract:Abstract ZSM-5 catalysts (C(X)-ZSM-5) with micropores and mesopores were prepared by a carbon templating method with a variation of carbon template content (X = 0, 10, 20, 30, 40, and 50 wt.%), and they were applied to the production of light olefins (ethylene and propylene) through catalytic cracking of C 5 Raffinate. The effect of carbon template content on the physicochemical properties and catalytic activity of C(X)-ZSM-5 catalysts was investigated. It was revealed that physicochemical properties of C(X)-ZSM-5 catalysts were strongly influenced by carbon template content. Adsorption ability for n-pentane and mesopore volume of C(X)-ZSM-5 catalysts increased with increasing carbon template content. It was also found that catalytic performance of C(X)-ZSM-5 catalysts was closely related to the mesoporosity of the catalyst. Conversion of C 5 Raffinate and yield for light olefins increased with increasing mesopore/micropore volume ratio of the catalyst, while selectivity for ethylene and propylene showed constant values. Thus, carbon template content in the C(X)-ZSM-5 catalysts strongly affected the mesoporosity of the catalyst, and in turn, mesoporosity played an important role in determining the catalytic performance in the production of light olefins through catalytic cracking of C 5 Raffinate.
Giuseppe Modolo - One of the best experts on this subject based on the ideXlab platform.
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applications of diglycolamide based solvent extraction processes in spent nuclear fuel reprocessing part 1 todga
Solvent Extraction and Ion Exchange, 2018Co-Authors: Daniel Whittaker, Andreas Geist, Robin J Taylor, Giuseppe Modolo, Mark Sarsfield, Andreas WildenAbstract:Over the last decade there has been much interest in the applications of diglycolamide (DGA) ligands for the extraction of the trivalent lanthanide and actinide ions from PUREX high active raffinat...
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direct selective extraction of trivalent americium from purex Raffinate using a combination of cyme4btphen and tedga a feasibility study
Solvent Extraction and Ion Exchange, 2017Co-Authors: Steve Lange, Andreas Wilden, Giuseppe Modolo, Fabian Sadowski, Markus Gerdes, Dirk BosbachAbstract:ABSTRACTThe direct and selective extraction of Am(III) from simulated PUREX Raffinate is demonstrated using a novel combination of the lipophilic extractant CyMe4BTPhen (2,9-bis(5,5,8,8-tetramethyl-5,6,7,8-tetrahydrobenzo[e]-[1,2,4]triazin-3-yl)-1,10-phenanthroline) and the hydrophilic complexant TEDGA (N,N,N’,N’-tetraethyl-diglycolamide) to enhance selectivity toward Am(III) extraction. Separation factors (SF) of up to SFAm/Cm = 4.9 were observed in tracer experiments using this combination of CyMe4BTPhen and TEDGA. Distribution ratios of stable isotopes of fission and activation products contained in a simulated PUREX Raffinate solution are reported for the first time with CyMe4BTPhen, and some co-extracted metal ions are identified. The metal ions partly co-extracted from the simulated PUREX Raffinate solution were Cu, Pd, Cd, Ag, Ni, and to a lesser extent Sn and Mo. The co-extraction of Pd and Ag was successfully suppressed using Bimet ((2S,2’S)-4,4’-(ethane-1,2-diylbis(sulfanediyl))bis(2-aminobutano...
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laboratory scale counter current centrifugal contactor demonstration of an innovative sanex process using a water soluble btp
Solvent Extraction and Ion Exchange, 2015Co-Authors: Andreas Wilden, Andreas Geist, Michal Sypula, Giuseppe Modolo, Steve Lange, Fabian Sadowski, D Magnusson, Peter Kaufholz, Udo Mullich, Dirk BosbachAbstract:In this paper the development and laboratory-scale demonstration of a novel “innovative-SANEX” (Selective Actinide Extraction) process using annular centrifugal contactors is presented. In this strategy, a solvent comprising the N,N,N’,N’-tetraoctyldiglycolamide (TODGA) extractant with addition of 5 vol.-% 1-octanol showed very good extraction efficiency of Am(III) and Cm(III) together with the trivalent lanthanides (Ln(III)) from simulated Plutonium Uranium Refining by Extraction (PUREX) Raffinate solution without 3rd phase formation. Cyclohexanediaminetetraacetic acid (CDTA) was used as masking agent to prevent the co-extraction of Zr and Pd. An(III) and Ln(III) were co-extracted from simulated PUREX Raffinate, and the loaded solvent was subjected to several stripping steps. The An(III) were selectively stripped using the hydrophilic complexing agent SO3-Ph-BTP (2,6-bis(5,6-di(sulfophenyl)-1,2,4-triazin-3-yl)pyridine). For the subsequent stripping of the Ln(III), a citric acid based solution was used. A...
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direct selective extraction of actinides iii from purex Raffinate using a mixture of cyme4 btbp and todga as 1 cycle sanex solvent part ii flow sheet design for a counter current centrifugal contactor demonstration process
Solvent Extraction and Ion Exchange, 2013Co-Authors: D Magnusson, Andreas Geist, Andreas Wilden, Giuseppe ModoloAbstract:The 1-cycle SANEX process has been developed as a simplification of the DIAMEX+SANEX concept by reducing the required process steps from two to one. The goal is to separate americium(III) and curium(III) directly from a PUREX Raffinate which is very complicated due to the complex composition of the solution. In previous work, extensive batch studies have been carried out using an organic phase comprising CyMe4-BTBP and TODGA. This system has now been further developed towards a counter-current centrifugal contactor test using a synthetic PUREX Raffinate solution. Single stage experiments were carried out to study the extraction kinetics and a 32 stage flow-sheet is proposed with calculated recoveries for some key elements. The calculations show that americium is recovered in the product with only small amounts of impurities. A demonstration process following the designed flow-sheet is expected to fulfill all the requirements for this complicated separation.
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use of polyaminocarboxylic acids as hydrophilic masking agents for fission products in actinide partitioning processes
Solvent Extraction and Ion Exchange, 2012Co-Authors: Michal Sypula, Andreas Geist, Andreas Wilden, C Schreinemachers, Rikard Malmbeck, Robin J Taylor, Giuseppe ModoloAbstract:During the partitioning of trivalent actinides from High Active Raffinate (HAR) solutions, most processes have to cope with an undesirable co-extraction of some of the fission products. Four hydrophilic complexing agents of the group of polyaminocarboxylic acids, namely EDTA, HEDTA, DTPA, and CTDA were tested and compared for their ability to complex fission products in a simulated PUREX Raffinate solution, thereby preventing their extraction into an organic solvent. Several solvents, based on TODGA and the DIAMEX reference molecule DMDOHEMA, that are commonly known to show quite high Zr and Pd co-extraction, were studied. Our investigations ultimately resulted in a substitution of oxalic acid and HEDTA by cyclohexanediaminetetraacetic acid (CDTA). A small addition of this hydrophilic complexing agent to the feed decreased the distribution ratios of Zr from 100 to 90% of the metal retained in the feed solution. The extraction of trivalent...
Yong Seung Kim - One of the best experts on this subject based on the ideXlab platform.
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a synergistic effect of α bi2mo3o12 and γ bi2moo6 catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Journal of Molecular Catalysis A-chemical, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, Howon Lee, In Kyu SongAbstract:Abstract α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were prepared by a co-precipitation method for use in the oxidative dehydrogenation of C 4 Raffinate-3 to 1,3-butadiene. A series of mixed catalysts composed of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 were also prepared by a mechanical mixing method to investigate any synergistic effects of α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3. The α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts were formed successfully, as confirmed by XRD, FT-IR, Raman spectroscopy, and ICP-AES analyses. The γ-Bi 2 MoO 6 catalyst exhibited a better catalytic performance than the α-Bi 2 Mo 3 O 12 catalyst due to its facile oxygen mobility. The conversion of n-butene and the yield for 1,3-butadine over the mixed catalysts showed volcano-shaped curves with respect to γ-Bi 2 MoO 6 content due to the synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts. Among the mixed catalysts, the catalyst composed of 10 wt.% α-Bi 2 Mo 3 O 12 and 90 wt.% γ-Bi 2 MoO 6 showed the best catalytic performance. The γ-Bi 2 MoO 6 catalyst retained a higher oxygen mobility than the α-Bi 2 Mo 3 O 12 catalyst, while the α-Bi 2 Mo 3 O 12 catalyst retained much more adsorption sites for n -butene than the γ-Bi 2 MoO 6 catalyst. The synergistic effect of the α-Bi 2 Mo 3 O 12 and γ-Bi 2 MoO 6 catalysts in the oxidative dehydrogenation of C 4 Raffinate-3 was due to a combination of the facile oxygen mobility of γ-Bi 2 MoO 6 and the abundant adsorption sites of α-Bi 2 Mo 3 O 12 for n -butene.
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catalytic performance of bismuth molybdate catalysts in the oxidative dehydrogenation of c4 Raffinate 3 to 1 3 butadiene
Applied Catalysis A-general, 2007Co-Authors: Ji Chul Jung, Heesoo Kim, Yong Seung Kim, Youngmin Chung, Tae Jin Kim, Seong Jun Lee, In Kyu SongAbstract:Abstract α-Bi2Mo3O12 and γ-Bi2MoO6 were prepared by a co-precipitation method, and were applied to the oxidative dehydrogenation of C4 Raffinate-3 to 1,3-butadiene. Both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts were thermally and structurally stable during the catalytic reaction. They exhibited a stable catalytic performance in the oxidative dehydrogenation of C4 Raffinate-3 without catalyst deactivation. However, the catalytic performance of γ-Bi2MoO6 was superior to α-Bi2Mo3O12 due to the facile oxygen mobility of γ-Bi2MoO6. The reactivity of n-butene isomers in the C4 Raffinate-3 decreased in the order of 1-butene > trans-2-butene > cis-2-butene over both α-Bi2Mo3O12 and γ-Bi2MoO6 catalysts. Steam played an essential role in suppressing CO2 formation, and furthermore, served as a heat sink for preventing hot spots or reactor run-away. In the catalytic reaction with respect to reaction temperature, the maximum conversion of n-butene (ca. 66%) and the maximum yield for 1,3-butadiene (ca. 60%) were achieved at 440 °C over the γ-Bi2MoO6 catalyst (n-butene:oxygen:steam = 1:0.75:15).
