Micro-channel reactor for steam reforming of methanol

Kundu, Aritra; Park, J.M.; Ahn, Ji Eun; Park, S.S.; Shul, Yong Gun; Han, Haksoo

doi:10.1016/j.fuel.2006.08.003

Cited by 62 publications

(19 citation statements)

References 14 publications

Supporting

Mentioning

Contrasting

Order By: Relevance

“…Recently, many morphological studies on small-sized catalytic combustors, which are called microchannel catalytic combustors [2][3][4][5], have been conducted. A microchannel combustor has the advantage of higher mass transfer and higher surface area per volume.…”

Section: Extended Abstractmentioning

confidence: 99%

“…A microchannel combustor has the advantage of higher mass transfer and higher surface area per volume. Kundu et al reported sol of alumina and zirconia on the etched stainless steal micro-channel for steaming reforming of methanol produced better stability and performance [2], but the durability of catalyst was weak. The energy generated in the combustion channel was insufficient because of higher reaction temperature, so extra cartridge heaters provided extra heat.…”

Section: Extended Abstractmentioning

confidence: 99%

“…When some parts of the catalytic combustor have hot spots with higher local temperatures, the combustor durability maybe affected or the reforming catalyst would be damaged, resulting in NOx generation [1]. Therefore, it is very important for a catalytic combustor that transfers heat into a reforming reactor to have a uniform temperature distribution.Recently, many morphological studies on small-sized catalytic combustors, which are called microchannel catalytic combustors [2][3][4][5], have been conducted. A microchannel combustor has the advantage of higher mass transfer and higher surface area per volume.…”

mentioning

confidence: 99%

See 2 more Smart Citations

Development of a Catalytic Combustor with Thin-Honeycomb Substrate

Choi¹,

Park²,

Kim³

2017

World Congress on Momentum, Heat and Mass Transfer

View full text Add to dashboard Cite

Extended AbstractTo obtain the most stable H2 yields in reforming systems, it is important to maintain a steady reaction temperature for catalytic reforming. When some parts of the catalytic combustor have hot spots with higher local temperatures, the combustor durability maybe affected or the reforming catalyst would be damaged, resulting in NOx generation [1]. Therefore, it is very important for a catalytic combustor that transfers heat into a reforming reactor to have a uniform temperature distribution.Recently, many morphological studies on small-sized catalytic combustors, which are called microchannel catalytic combustors [2][3][4][5], have been conducted. A microchannel combustor has the advantage of higher mass transfer and higher surface area per volume. Kundu et al. reported sol of alumina and zirconia on the etched stainless steal micro-channel for steaming reforming of methanol produced better stability and performance [2], but the durability of catalyst was weak. The energy generated in the combustion channel was insufficient because of higher reaction temperature, so extra cartridge heaters provided extra heat. It is commonly very difficult to make a coating layer of catalysts for combustion and reforming reactions as micro-channels are made of metal or alumina materials. Particularly, catalysts coated on metal or on alumina are detached easily and have very low durability. After combustion or reforming, catalysts lose their activation energy and have to be replaced, resulting in high economic losses.The objective this study is to optimize the catalytic combustor using a thin-honeycomb ceramic substrate, which is capable of providing a dimethyl ether (DME) reformer with a heat source required for endothermic reforming process. The catalytic combustor can also maintain a uniform temperature distribution about 500℃. The catalytic combustor was set the type of a fixed-bed flow reactor under atmospheric pressure. Pt/ γ -Al2O3 catalyst was coated on the cordierite substrate (600 cpsi). The experimental variables are the composition of multi-catalyst blocks, flow distributor, space velocity, excess air ratio, exit cross-section ratio of the burner, and type of fuel.From the results, it was found that the space velocity was selected at the range of 18,000-27,000 h -1 for stable combustion (RMSE(root mean square energy) <10). For the catalytic combustor using C3H8 as fuel, the design combination for the best performance with temperature uniformity and with no exhaust pollutants was the optimized Tshaped and SiC foam distributor, 3 catalyst blocks(lean coating on the front catalyst and rich coating on the rear of catalyst blocks), and 50% minimum cross-section ratio of the combustor outlet. For the catalytic combustor fueled with DME, the temperature variation on the surface of the catalytic combustor could be maintained within 17.6℃ compared to the reference temperature.

show abstract

Section: Extended Abstractmentioning

confidence: 99%

Section: Extended Abstractmentioning

confidence: 99%

mentioning

confidence: 99%

See 1 more Smart Citation

Development of a Catalytic Combustor with Thin-Honeycomb Substrate

Choi¹,

Park²,

Kim³

2017

World Congress on Momentum, Heat and Mass Transfer

View full text Add to dashboard Cite

show abstract

“…Research work involves analysis of process economics [9], optimization of reactor design [10,11], optimization of operation conditions [12,13], thermodynamic analysis [14,15], catalysts used in steam reforming [16][17][18][19][20], and reaction mechanism of simulated species [21,22].…”

Section: Introductionmentioning

confidence: 99%

Steam Reforming of Bio‐Oil for Hydrogen Production: Effect of Ni‐Co Bimetallic Catalysts

Zhang

et al. 2011

Chem Eng & Technol

View full text Add to dashboard Cite

Various Ni-Co bimetallic catalysts were prepared by incorporating sol-gel and wet impregnation methods. A laboratory-scale fixed-bed reactor was employed to investigate their effects on hydrogen production from steam reforming of bio-oil. The catalyst causes the condensation reaction of bio-oil, which generates coke and inhibits the formation of gas at temperatures of 250°C and 350°C. At 450°C and above the transformation of bio-oil is initiated and gaseous products are generated. The catalyst also can promote the generation of H 2 as well as the transformation of CO and CH 4 and plays an active role in steam reforming of bio-oil or gaseous products from bio-oil pyrolysis. The developed 3Ni9Co/Ce-Zr-O catalyst achieved maximum hydrogen yield and lowest coke formation rate and provided a better stability than a commercial Ni-based catalyst.

show abstract

“…Bio-oil produced from fast pyrolysis of biomass represents a type of high-energy density chemical and, in addition, ease of transport and generation of hydrogen via steam reforming of this bio-oil on-site where the hydrogen is needed can be achieved [2]. In recent years, some research institutions have studied the steam reforming of bio-oil with regard to reactor design [3], optimization of technological conditions [4,5], thermodynamic analysis [4,6], and the preparation and modification of reforming catalysts [7][8][9][10][11][12][13][14][15][16].…”

Section: Introductionmentioning

confidence: 99%

A Comparison of Steam Reforming of Two Model Bio‐Oil Fractions

Sui

Yan

2008

Chem Eng & Technol

View full text Add to dashboard Cite

Two model bio-oil fractions were chosen as two different major classes of components present in bio-oil. Steam reforming of the two fractions was carried out to investigate the gas product distributions and carbon deposition behavior. Higher H 2 yield and carbon conversion to the gaseous phase can be obtained at relatively low temperature (650°C) for steam reforming of the light fraction. For steam reforming of the heavy fraction, a higher temperature (800°C) is necessary to obtain higher H 2 yield and carbon conversion to the gaseous phase. At 800°C, the heavy fraction requires a higher steam to carbon ratio (10) than that for the light fraction (7) to achieve efficient steam reforming. Based on the same carbon space velocity, for 10 h stream time, the drop of H 2 yield and carbon conversion to the gaseous phase in the steam reforming of the heavy fraction is more rapid than that of the light fraction. Carbon deposition in the steam reforming of the heavy fraction is much more severe than that of the light fraction, as determined by carbon content analysis and SEM detection.

show abstract

Micro-channel reactor for steam reforming of methanol

Cited by 62 publications

References 14 publications

Development of a Catalytic Combustor with Thin-Honeycomb Substrate

Development of a Catalytic Combustor with Thin-Honeycomb Substrate

Steam Reforming of Bio‐Oil for Hydrogen Production: Effect of Ni‐Co Bimetallic Catalysts

A Comparison of Steam Reforming of Two Model Bio‐Oil Fractions

Contact Info

Product

Resources

About