Characteristics of an Integrated Micro Packed Bed Reactor-Heat Exchanger for methanol synthesis from syngas

Bakhtiary-Davijany, Hamidreza; Hayer, Fatemeh; Phan, Xuyen Kim; Myrstad, Rune; Venvik, Hilde J.; Pfeifer, Peter; Holmén, Anders

doi:10.1016/j.cej.2010.08.074

Cited by 70 publications

(38 citation statements)

References 18 publications

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“…9c), under constant bed porosity, permeability, particle size and gas temperature. It shows that even if an increase in the gas velocity leads to higher pressure drop, this effect remains relatively small over the flow range applied (GHSV of 3,000-45,000 NmL/gcat/h), in agreement with experimental results [25,26].…”

Section: Variation Of Reaction Slit Dimensionssupporting

confidence: 79%

“…Details on the fabrication of this reactor have been described elsewhere [22,[24][25][26]. Reactors with eight reaction slits (8-slit reactors) of a different cross section of 8.8 9 0.8 mm 2 and with nine adjacent cooling channels were applied for performance assessment, and the reaction slits were equipped with hexagonally arranged pillars throughout the slits in order to facilitate heat transfer and flow distribution [25].…”

Section: Reactor Geometrymentioning

confidence: 99%

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Modeling and Simulation of an Integrated Micro Packed Bed Reactor-Heat Exchanger Configuration for Direct Dimethyl Ether Synthesis

et al. 2011

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The application of an integrated micro packed bed reactor-heat exchanger for highly exothermic syngas conversion to dimethyl ether was investigated by numerical simulation. A three-dimensional pseudo-homogeneous model was developed to describe concentration and temperature distributions inside a single reaction slit. The model was adopted at low Reynolds numbers (small catalyst particles and long residence times). The simulation results reveal that the micro packed reaction slit is close to isothermal, and a negligible temperature gradient is predicted also for a doubling of the critical reaction slit dimension, i.e. the reaction slit height. The flow in the reaction slit was modelled by Brinkman's equation and it was found that the pressure drop in wide range of gas velocity was not significant. The reactor simulation showed good agreement with experimental results and could be further developed to assess the potential of microstructured packed bed reactors to intensify large-scale industrial processes.

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Section: Variation Of Reaction Slit Dimensionssupporting

confidence: 79%

Section: Reactor Geometrymentioning

confidence: 99%

Modeling and Simulation of an Integrated Micro Packed Bed Reactor-Heat Exchanger Configuration for Direct Dimethyl Ether Synthesis

et al. 2011

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“…The reactor consists of a 6 cm long reaction slit with rectangular cross section of 8.8 × 1.5 mm 2 , sandwiched between cross flow channels for circulation of a heat transfer oil. Such reactors have been studied earlier under similar operating conditions for the methanol [21][22][23] and the direct DME [24][25][26] syntheses, and established as practically isothermal, isobaric, free from mass transfer limitations, and with a narrow residence time distribution. Premixed synthesis gas with H 2 to CO molar ratio of either 1 (Syngas-1) or 2 (Syngas-2) was used as feed.…”

Section: Methodsmentioning

confidence: 99%

Direct dimethyl ether synthesis from synthesis gas: The influence of methanol dehydration on methanol synthesis reaction

et al. 2016

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Direct dimethyl ether (DME) synthesis from synthesis gas is studied with regard to potential effects of methanol dehydration on methanol formation and copperbased catalyst performance. For this, the influence of the operating conditions (space velocity, temperature, pressure, time-on-stream and syngas composition) on activity, selectivity and stability of the catalyst was studied and compared for methanol synthesis and direct DME synthesis. The advantage of the direct over the two-step DME synthesis is apparent at conditions where syngas conversion to methanol is thermodynamically limited. However, under the applied operating conditions, results suggest that combining methanol synthesis and dehydration has a negative effect on the methanol formation kinetics. The origin of the observed phenomena is investigated by varying dehydration catalyst and by introducing dehydration products (DME and water) into the methanol synthesis feed. Choice of the solid acid catalyst does not seem to affect methanol formation, and DME is also found to be practically inert over the methanol synthesis catalysts. Water injection, on the other hand, led to a significant decrease in the methanol synthesis rate. Thus, formation of an additional amount of water through methanol dehydration might be an explanation for the lower methanol formation rate in the direct DME synthesis.

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“…For example, NG accounts for 20% of hydrocarbon-related CO 2 emissions (Abbas and Wan Daud, 2010). On the other hand, a considerable amount of stranded gas reserves are located off shore with low economic incentive to be produced, transported and sold (Bakhtiary-Davijany et al, 2011). In these circumstances, the natural gas that often comes out of the earth along with crude oil is burned off in flares.…”

Section: Natural Gasmentioning

confidence: 99%

A comparative study of two different membranes applied for auto-thermal methanol synthesis process

Rahmani

Haghighi

Estifaee

et al. 2012

Journal of Natural Gas Science and Engineering

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Characteristics of an Integrated Micro Packed Bed Reactor-Heat Exchanger for methanol synthesis from syngas

Cited by 70 publications

References 18 publications

Modeling and Simulation of an Integrated Micro Packed Bed Reactor-Heat Exchanger Configuration for Direct Dimethyl Ether Synthesis

Modeling and Simulation of an Integrated Micro Packed Bed Reactor-Heat Exchanger Configuration for Direct Dimethyl Ether Synthesis

Direct dimethyl ether synthesis from synthesis gas: The influence of methanol dehydration on methanol synthesis reaction

A comparative study of two different membranes applied for auto-thermal methanol synthesis process

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