The Experts below are selected from a list of 186 Experts worldwide ranked by ideXlab platform
In Kyu Song - One of the best experts on this subject based on the ideXlab platform.
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hydrogen production by steam reforming of liquefied natural gas lng over trimethylbenzene assisted ordered mesoporous nickel alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over trimethylbenzene-assisted ordered mesoporous nickel–alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over mesoporous alkaline earth metal-promoted nickel-alumina xerogel catalysts
Journal of Molecular Catalysis A: Chemical, 2013Co-Authors: Jaekyeong Yoo, Yongju Bang, Seung Ju Han, Tae Hun Kang, Jinwon Lee, In Kyu SongAbstract:Abstract A series of mesoporous alkaline earth metal-promoted nickel-alumina xerogel (M/NA, M = Mg, Ca, Sr, and Ba) catalysts were prepared by a single-step epoxide-driven sol–gel method and a subsequent incipient wetness impregnation method. They were applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For reference, a nickel-alumina xerogel catalyst without promoter (NA) was prepared by a single-step epoxide-driven sol–gel method. The catalysts were characterized by N 2 adsorption–desorption, ICP-AES, XRD, TPR, H 2 -chemisorption, TEM, and CHNS analyses. Surface area and pore volume of M/NA catalysts were smaller than those of NA catalyst due to blockage of mesopores by promoters during the impregnation step. Both NA and M/NA catalysts exhibited X-ray diffraction patterns corresponding to nickel Aluminate Phase. In the TPR measurements, it was revealed that all the catalysts retained surface nickel Aluminate Phase, regardless of the identity of alkaline earth metal. Nickel surface area of reduced catalysts decreased in the order of Mg/NA > Sr/NA > Ca/NA > NA > Ba/NA. In the hydrogen production by steam reforming of LNG, the catalytic performance of NA and M/NA catalysts was well correlated with the nickel surface area of the catalysts; LNG conversion and hydrogen yield increased with increasing nickel surface area. Among the catalysts tested, Mg/NA catalyst with the highest nickel surface area showed the best catalytic performance. The amount of carbon deposition on the used M/NA catalysts was less than that on the used NA catalyst.
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Mesoporous Nickel–Alumina Catalysts for Hydrogen Production by Steam Reforming of Liquefied Natural Gas (LNG)
Catalysis Surveys from Asia, 2010Co-Authors: Jeong Gil Seo, Min Hye Youn, In Kyu SongAbstract:Recent progress on the mesoporous nickel–alumina catalysts for hydrogen production by steam reforming of liquefied natural gas (LNG) was reported in this review. A number of mesoporous nickel–alumina composite catalysts were prepared by a single-step surfactant-templating method using cationic, anionic, and non-ionic surfactant as structure-directing agents for use in hydrogen production by steam reforming of LNG. For comparison, nickel catalysts supported on mesoporous aluminas were also prepared by an impregnation method. The effect of preparation method and surfactant identity on physicochemical properties and catalytic activities of mesoporous nickel–alumina catalysts in the steam reforming of LNG was investigated. Regardless of preparation method and surfactant identity, nickel oxide species were finely dispersed on the surface of mesoporous nickel–alumina catalysts through the formation of surface nickel Aluminate Phase. However, nickel dispersion and nickel surface area of mesoporous nickel–alumina catalysts were strongly affected by the preparation method and surfactant identity. It was found that nickel surface area of mesoporous nickel–alumina catalyst served as one of the important factors determining the catalytic performance in hydrogen production by steam reforming of LNG. Among the catalysts tested, a mesoporous nickel–alumina composite catalyst prepared by a single-step non-ionic surfactant-templating method exhibited the best catalytic performance due to its highest nickel surface area.
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hydrogen production by steam reforming of liquefied natural gas over mesoporous ni al2o3 composite catalyst prepared by a single step non ionic surfactant templating method
Catalysis Letters, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Dong Ryul Park, In Kyu SongAbstract:A mesoporous Ni-Al2O3 composite catalyst (Ni-A-NS) was prepared by a single-step non-ionic surfactant-templating method for use in hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/A-NS) was also prepared by an impregnation method. The effect of physicochemical properties on the performance of Ni-A-NS catalyst in the steam reforming of LNG was investigated. Ni-A-NS catalyst retained superior textural properties compared to Ni/A-NS catalyst. Nickel oxide species were highly dispersed on the surface of both Ni/A-NS and Ni-A-NS catalysts through the formation of surface nickel Aluminate Phase. Although both Ni/A-NS and Ni-A-NS catalysts exhibited a stable catalytic performance, Ni-A-NS catalyst showed a better catalytic performance than Ni/A-NS catalyst in the steam reforming of LNG. High nickel surface area and high nickel dispersion of Ni-A-NS catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. High reducibility of Ni-A-NS catalyst was also responsible for its high catalytic performance.
Jeong Gil Seo - One of the best experts on this subject based on the ideXlab platform.
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hydrogen production by steam reforming of liquefied natural gas lng over trimethylbenzene assisted ordered mesoporous nickel alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over trimethylbenzene-assisted ordered mesoporous nickel–alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Mesoporous Nickel–Alumina Catalysts for Hydrogen Production by Steam Reforming of Liquefied Natural Gas (LNG)
Catalysis Surveys from Asia, 2010Co-Authors: Jeong Gil Seo, Min Hye Youn, In Kyu SongAbstract:Recent progress on the mesoporous nickel–alumina catalysts for hydrogen production by steam reforming of liquefied natural gas (LNG) was reported in this review. A number of mesoporous nickel–alumina composite catalysts were prepared by a single-step surfactant-templating method using cationic, anionic, and non-ionic surfactant as structure-directing agents for use in hydrogen production by steam reforming of LNG. For comparison, nickel catalysts supported on mesoporous aluminas were also prepared by an impregnation method. The effect of preparation method and surfactant identity on physicochemical properties and catalytic activities of mesoporous nickel–alumina catalysts in the steam reforming of LNG was investigated. Regardless of preparation method and surfactant identity, nickel oxide species were finely dispersed on the surface of mesoporous nickel–alumina catalysts through the formation of surface nickel Aluminate Phase. However, nickel dispersion and nickel surface area of mesoporous nickel–alumina catalysts were strongly affected by the preparation method and surfactant identity. It was found that nickel surface area of mesoporous nickel–alumina catalyst served as one of the important factors determining the catalytic performance in hydrogen production by steam reforming of LNG. Among the catalysts tested, a mesoporous nickel–alumina composite catalyst prepared by a single-step non-ionic surfactant-templating method exhibited the best catalytic performance due to its highest nickel surface area.
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hydrogen production by steam reforming of liquefied natural gas over mesoporous ni al2o3 composite catalyst prepared by a single step non ionic surfactant templating method
Catalysis Letters, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Dong Ryul Park, In Kyu SongAbstract:A mesoporous Ni-Al2O3 composite catalyst (Ni-A-NS) was prepared by a single-step non-ionic surfactant-templating method for use in hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/A-NS) was also prepared by an impregnation method. The effect of physicochemical properties on the performance of Ni-A-NS catalyst in the steam reforming of LNG was investigated. Ni-A-NS catalyst retained superior textural properties compared to Ni/A-NS catalyst. Nickel oxide species were highly dispersed on the surface of both Ni/A-NS and Ni-A-NS catalysts through the formation of surface nickel Aluminate Phase. Although both Ni/A-NS and Ni-A-NS catalysts exhibited a stable catalytic performance, Ni-A-NS catalyst showed a better catalytic performance than Ni/A-NS catalyst in the steam reforming of LNG. High nickel surface area and high nickel dispersion of Ni-A-NS catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. High reducibility of Ni-A-NS catalyst was also responsible for its high catalytic performance.
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hydrogen production by steam reforming of liquefied natural gas lng over mesoporous nickel alumina composite catalyst prepared by an anionic surfactant templating method
Catalysis Today, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Jin Suk Chung, Dong Ryul Park, Sunyoung Park, In Kyu SongAbstract:Abstract A mesoporous nickel–alumina composite catalyst (Ni–Al2O3) was prepared by an anionic surfactant-templating method, and was applied to hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/Al2O3) was prepared by an impregnation method. High surface area and well-developed mesopores of both Ni–Al2O3 and Ni/Al2O3 catalysts improved the dispersion of nickel species through the formation of nickel Aluminate Phase. In the Ni–Al2O3 catalyst, nickel species were homogeneously dispersed without significant pore blocking through the formation of Ni–O–Al composite structure. The Ni–Al2O3 catalyst was very efficient for suppressing the nickel sintering during the reduction process, resulting in enhanced nickel dispersion and active nickel surface area. Ni–Al2O3 catalyst showed a stable catalytic performance without significant catalyst deactivation during the reaction extending over 3000 min, while Ni/Al2O3 catalyst exhibited a stable catalytic performance at the initial stage but experienced a slight catalyst deactivation in the long run. The Ni–Al2O3 catalyst showed a better catalytic performance than the Ni/Al2O3 catalyst. High active nickel surface area and fine nickel dispersion of Ni–Al2O3 catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. Strong resistance of Ni–Al2O3 catalyst toward carbon deposition and nickel sintering was also responsible for its high catalytic performance.
Ji Chul Jung - One of the best experts on this subject based on the ideXlab platform.
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hydrogen production by steam reforming of liquefied natural gas lng over trimethylbenzene assisted ordered mesoporous nickel alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over trimethylbenzene-assisted ordered mesoporous nickel–alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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hydrogen production by steam reforming of liquefied natural gas over mesoporous ni al2o3 composite catalyst prepared by a single step non ionic surfactant templating method
Catalysis Letters, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Dong Ryul Park, In Kyu SongAbstract:A mesoporous Ni-Al2O3 composite catalyst (Ni-A-NS) was prepared by a single-step non-ionic surfactant-templating method for use in hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/A-NS) was also prepared by an impregnation method. The effect of physicochemical properties on the performance of Ni-A-NS catalyst in the steam reforming of LNG was investigated. Ni-A-NS catalyst retained superior textural properties compared to Ni/A-NS catalyst. Nickel oxide species were highly dispersed on the surface of both Ni/A-NS and Ni-A-NS catalysts through the formation of surface nickel Aluminate Phase. Although both Ni/A-NS and Ni-A-NS catalysts exhibited a stable catalytic performance, Ni-A-NS catalyst showed a better catalytic performance than Ni/A-NS catalyst in the steam reforming of LNG. High nickel surface area and high nickel dispersion of Ni-A-NS catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. High reducibility of Ni-A-NS catalyst was also responsible for its high catalytic performance.
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hydrogen production by steam reforming of liquefied natural gas lng over mesoporous nickel alumina composite catalyst prepared by an anionic surfactant templating method
Catalysis Today, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Jin Suk Chung, Dong Ryul Park, Sunyoung Park, In Kyu SongAbstract:Abstract A mesoporous nickel–alumina composite catalyst (Ni–Al2O3) was prepared by an anionic surfactant-templating method, and was applied to hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/Al2O3) was prepared by an impregnation method. High surface area and well-developed mesopores of both Ni–Al2O3 and Ni/Al2O3 catalysts improved the dispersion of nickel species through the formation of nickel Aluminate Phase. In the Ni–Al2O3 catalyst, nickel species were homogeneously dispersed without significant pore blocking through the formation of Ni–O–Al composite structure. The Ni–Al2O3 catalyst was very efficient for suppressing the nickel sintering during the reduction process, resulting in enhanced nickel dispersion and active nickel surface area. Ni–Al2O3 catalyst showed a stable catalytic performance without significant catalyst deactivation during the reaction extending over 3000 min, while Ni/Al2O3 catalyst exhibited a stable catalytic performance at the initial stage but experienced a slight catalyst deactivation in the long run. The Ni–Al2O3 catalyst showed a better catalytic performance than the Ni/Al2O3 catalyst. High active nickel surface area and fine nickel dispersion of Ni–Al2O3 catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. Strong resistance of Ni–Al2O3 catalyst toward carbon deposition and nickel sintering was also responsible for its high catalytic performance.
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Effect of preparation method of mesoporous Ni–Al2O3 catalysts on their catalytic activity for hydrogen production by steam reforming of liquefied natural gas (LNG)
International Journal of Hydrogen Energy, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, In Kyu SongAbstract:Abstract Mesoporous Ni–Al 2 O 3 catalysts were prepared by impregnation method (NiAl-IP), co-precipitation method (NiAl-CP), and sequential precipitation method (NiAl-SP) for use in hydrogen production by steam reforming of liquefied natural gas (LNG). The effect of preparation method of mesoporous Ni–Al 2 O 3 catalysts on their catalytic activity for steam reforming of LNG was investigated. Physicochemical properties of Ni–Al 2 O 3 catalysts were strongly influenced by the preparation method of Ni–Al 2 O 3 catalysts. Surface area, pore volume, and average pore size of Ni–Al 2 O 3 catalysts decreased in the order of NiAl-SP > NiAl-CP > NiAl-IP. Nickel species strongly interacted with Al 2 O 3 supports through the formation of nickel Aluminate Phase. Surface nickel Aluminate Phase of Ni–Al 2 O 3 catalysts was readily reduced after the reduction process, while bulk nickel Aluminate Phase of NiAl-CP catalyst was hardly reducible. Nickel dispersion and nickel surface area of Ni–Al 2 O 3 catalysts decreased in the order of NiAl-SP > NiAl-CP > NiAl-IP. Among the catalysts tested, NiAl-SP catalyst with the highest nickel surface area showed the best catalytic performance in the steam reforming of LNG. Furthermore, finely dispersed nickel species in the NiAl-SP catalyst efficiently suppressed the carbon deposition during the reaction.
Min Hye Youn - One of the best experts on this subject based on the ideXlab platform.
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Mesoporous Nickel–Alumina Catalysts for Hydrogen Production by Steam Reforming of Liquefied Natural Gas (LNG)
Catalysis Surveys from Asia, 2010Co-Authors: Jeong Gil Seo, Min Hye Youn, In Kyu SongAbstract:Recent progress on the mesoporous nickel–alumina catalysts for hydrogen production by steam reforming of liquefied natural gas (LNG) was reported in this review. A number of mesoporous nickel–alumina composite catalysts were prepared by a single-step surfactant-templating method using cationic, anionic, and non-ionic surfactant as structure-directing agents for use in hydrogen production by steam reforming of LNG. For comparison, nickel catalysts supported on mesoporous aluminas were also prepared by an impregnation method. The effect of preparation method and surfactant identity on physicochemical properties and catalytic activities of mesoporous nickel–alumina catalysts in the steam reforming of LNG was investigated. Regardless of preparation method and surfactant identity, nickel oxide species were finely dispersed on the surface of mesoporous nickel–alumina catalysts through the formation of surface nickel Aluminate Phase. However, nickel dispersion and nickel surface area of mesoporous nickel–alumina catalysts were strongly affected by the preparation method and surfactant identity. It was found that nickel surface area of mesoporous nickel–alumina catalyst served as one of the important factors determining the catalytic performance in hydrogen production by steam reforming of LNG. Among the catalysts tested, a mesoporous nickel–alumina composite catalyst prepared by a single-step non-ionic surfactant-templating method exhibited the best catalytic performance due to its highest nickel surface area.
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hydrogen production by steam reforming of liquefied natural gas over mesoporous ni al2o3 composite catalyst prepared by a single step non ionic surfactant templating method
Catalysis Letters, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Dong Ryul Park, In Kyu SongAbstract:A mesoporous Ni-Al2O3 composite catalyst (Ni-A-NS) was prepared by a single-step non-ionic surfactant-templating method for use in hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/A-NS) was also prepared by an impregnation method. The effect of physicochemical properties on the performance of Ni-A-NS catalyst in the steam reforming of LNG was investigated. Ni-A-NS catalyst retained superior textural properties compared to Ni/A-NS catalyst. Nickel oxide species were highly dispersed on the surface of both Ni/A-NS and Ni-A-NS catalysts through the formation of surface nickel Aluminate Phase. Although both Ni/A-NS and Ni-A-NS catalysts exhibited a stable catalytic performance, Ni-A-NS catalyst showed a better catalytic performance than Ni/A-NS catalyst in the steam reforming of LNG. High nickel surface area and high nickel dispersion of Ni-A-NS catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. High reducibility of Ni-A-NS catalyst was also responsible for its high catalytic performance.
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hydrogen production by steam reforming of liquefied natural gas lng over mesoporous nickel alumina composite catalyst prepared by an anionic surfactant templating method
Catalysis Today, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, Jin Suk Chung, Dong Ryul Park, Sunyoung Park, In Kyu SongAbstract:Abstract A mesoporous nickel–alumina composite catalyst (Ni–Al2O3) was prepared by an anionic surfactant-templating method, and was applied to hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, a nickel catalyst supported on mesoporous alumina (Ni/Al2O3) was prepared by an impregnation method. High surface area and well-developed mesopores of both Ni–Al2O3 and Ni/Al2O3 catalysts improved the dispersion of nickel species through the formation of nickel Aluminate Phase. In the Ni–Al2O3 catalyst, nickel species were homogeneously dispersed without significant pore blocking through the formation of Ni–O–Al composite structure. The Ni–Al2O3 catalyst was very efficient for suppressing the nickel sintering during the reduction process, resulting in enhanced nickel dispersion and active nickel surface area. Ni–Al2O3 catalyst showed a stable catalytic performance without significant catalyst deactivation during the reaction extending over 3000 min, while Ni/Al2O3 catalyst exhibited a stable catalytic performance at the initial stage but experienced a slight catalyst deactivation in the long run. The Ni–Al2O3 catalyst showed a better catalytic performance than the Ni/Al2O3 catalyst. High active nickel surface area and fine nickel dispersion of Ni–Al2O3 catalyst played an important role in enhancing the dehydrogenation reaction of hydrocarbon species and the gasification reaction of adsorbed carbon species in the steam reforming of LNG. Strong resistance of Ni–Al2O3 catalyst toward carbon deposition and nickel sintering was also responsible for its high catalytic performance.
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Hydrogen Production by Steam Reforming of Liquefied Natural Gas over Mesoporous Ni-Al2O3 Catalysts Prepared by a Co-Precipitation Method: Effect of Ni/Al Atomic Ratio
Catalysis Letters, 2009Co-Authors: Jeong Gil Seo, Min Hye Youn, Insung Nam, Sunhwan Hwang, Jin Suk Chung, In Kyu SongAbstract:Mesoporous Ni-Al2O3 (XNiAl) catalysts with different Ni/Al atomic ratio (X) were prepared by a co-precipitation method for use in hydrogen production by steam reforming of liquefied natural gas (LNG). The effect of Ni/Al atomic ratio of mesoporous XNiAl catalysts on their physicochemical properties and catalytic activity for steam reforming of LNG was investigated. Physical properties of XNiAl catalysts did not show a consistent trend with respect to Ni/Al atomic ratio, while chemical properties of XNiAl catalysts strongly influenced by Ni/Al atomic ratio. Nickel species were highly dispersed on the surface of XNiAl catalysts through the formation of nickel Aluminate Phase or solid solution of nickel oxide and nickel Aluminate Phase. In the steam reforming of LNG, both LNG conversion and hydrogen composition in dry gas showed volcano-shaped curves with respect to Ni/Al atomic ratio. Nickel surface area of XNiAl catalysts was well correlated with LNG conversion and hydrogen composition over the catalysts. Among the catalysts tested, 0.8NiAl (Ni/Al = 0.8) catalyst with the highest nickel surface area showed the best catalytic performance.
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Effect of preparation method of mesoporous Ni–Al2O3 catalysts on their catalytic activity for hydrogen production by steam reforming of liquefied natural gas (LNG)
International Journal of Hydrogen Energy, 2009Co-Authors: Jeong Gil Seo, Ji Chul Jung, Min Hye Youn, In Kyu SongAbstract:Abstract Mesoporous Ni–Al 2 O 3 catalysts were prepared by impregnation method (NiAl-IP), co-precipitation method (NiAl-CP), and sequential precipitation method (NiAl-SP) for use in hydrogen production by steam reforming of liquefied natural gas (LNG). The effect of preparation method of mesoporous Ni–Al 2 O 3 catalysts on their catalytic activity for steam reforming of LNG was investigated. Physicochemical properties of Ni–Al 2 O 3 catalysts were strongly influenced by the preparation method of Ni–Al 2 O 3 catalysts. Surface area, pore volume, and average pore size of Ni–Al 2 O 3 catalysts decreased in the order of NiAl-SP > NiAl-CP > NiAl-IP. Nickel species strongly interacted with Al 2 O 3 supports through the formation of nickel Aluminate Phase. Surface nickel Aluminate Phase of Ni–Al 2 O 3 catalysts was readily reduced after the reduction process, while bulk nickel Aluminate Phase of NiAl-CP catalyst was hardly reducible. Nickel dispersion and nickel surface area of Ni–Al 2 O 3 catalysts decreased in the order of NiAl-SP > NiAl-CP > NiAl-IP. Among the catalysts tested, NiAl-SP catalyst with the highest nickel surface area showed the best catalytic performance in the steam reforming of LNG. Furthermore, finely dispersed nickel species in the NiAl-SP catalyst efficiently suppressed the carbon deposition during the reaction.
Yongju Bang - One of the best experts on this subject based on the ideXlab platform.
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hydrogen production by steam reforming of liquefied natural gas lng over trimethylbenzene assisted ordered mesoporous nickel alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over trimethylbenzene-assisted ordered mesoporous nickel–alumina catalyst
International Journal of Hydrogen Energy, 2013Co-Authors: Yongju Bang, Seung Ju Han, Jaekyeong Yoo, Jung Ho Choi, Ki Hyuk Kang, Ji Hwan Song, Jeong Gil Seo, Ji Chul Jung, In Kyu SongAbstract:Abstract A trimethylbenzene (TMB)-assisted ordered mesoporous nickel–alumina catalyst (denoted as TNA) was prepared by a single-step evaporation-induced self-assembly (EISA) method, and it was applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For comparison, an ordered mesoporous nickel–alumina catalyst (denoted as NA) was also prepared by a single-step EISA method in the absence of TMB. Pore volume and average pore diameter of TNA catalyst were larger than those of NA catalyst due to structural modification caused by TMB addition in the preparation of TNA catalyst. In addition, TNA catalyst showed less ordered mesoporous array than NA catalyst. Both NA and TNA catalysts exhibited diffraction patterns corresponding to nickel Aluminate Phase, and they retained surface nickel Aluminate Phase with high stability and reducibility. Crystallite size of metallic nickel in the reduced TNA catalyst was smaller than that in the reduced NA catalyst due to strong nickel–alumina interaction of surface nickel Aluminate Phase over TNA catalyst. In the hydrogen production by steam reforming of LNG, TNA catalyst with small crystallite size of metallic nickel showed a better catalytic performance than NA catalyst in terms of LNG conversion and hydrogen yield. Furthermore, steam reforming reaction rather than water–gas shift reaction favorably occurred over TNA catalyst.
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Hydrogen production by steam reforming of liquefied natural gas (LNG) over mesoporous alkaline earth metal-promoted nickel-alumina xerogel catalysts
Journal of Molecular Catalysis A: Chemical, 2013Co-Authors: Jaekyeong Yoo, Yongju Bang, Seung Ju Han, Tae Hun Kang, Jinwon Lee, In Kyu SongAbstract:Abstract A series of mesoporous alkaline earth metal-promoted nickel-alumina xerogel (M/NA, M = Mg, Ca, Sr, and Ba) catalysts were prepared by a single-step epoxide-driven sol–gel method and a subsequent incipient wetness impregnation method. They were applied to the hydrogen production by steam reforming of liquefied natural gas (LNG). For reference, a nickel-alumina xerogel catalyst without promoter (NA) was prepared by a single-step epoxide-driven sol–gel method. The catalysts were characterized by N 2 adsorption–desorption, ICP-AES, XRD, TPR, H 2 -chemisorption, TEM, and CHNS analyses. Surface area and pore volume of M/NA catalysts were smaller than those of NA catalyst due to blockage of mesopores by promoters during the impregnation step. Both NA and M/NA catalysts exhibited X-ray diffraction patterns corresponding to nickel Aluminate Phase. In the TPR measurements, it was revealed that all the catalysts retained surface nickel Aluminate Phase, regardless of the identity of alkaline earth metal. Nickel surface area of reduced catalysts decreased in the order of Mg/NA > Sr/NA > Ca/NA > NA > Ba/NA. In the hydrogen production by steam reforming of LNG, the catalytic performance of NA and M/NA catalysts was well correlated with the nickel surface area of the catalysts; LNG conversion and hydrogen yield increased with increasing nickel surface area. Among the catalysts tested, Mg/NA catalyst with the highest nickel surface area showed the best catalytic performance. The amount of carbon deposition on the used M/NA catalysts was less than that on the used NA catalyst.
