Methanol synthesis in a trickle‐bed reactor

Pass, Geoffrey; Holzhauser, Craig; Akgerman, Aydin; Anthony, R.G.

doi:10.1002/aic.690360712

“…Fixed fluidized or circulating, fluidized reactor types would ensure good temperature control and eliminate diffusion restrictions [371], but the mechanical strength of the present methanol synthesis catalyst is not sufficient in the reduced state to avoid the generation of excessive amounts of fines. Fixed fluidized or circulating, fluidized reactor types would ensure good temperature control and eliminate diffusion restrictions [371], but the mechanical strength of the present methanol synthesis catalyst is not sufficient in the reduced state to avoid the generation of excessive amounts of fines.…”

Section: Reactor Systems and Synthesis Loop Layoutmentioning

confidence: 99%

Methanol Synthesis

Hansen¹,

Nielsen²

2008

Handbook of Heterogeneous Catalysis

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The sections in this article are Introduction Thermodynamics Methanol Synthesis Catalysts Introduction Zn O / Cr 2 O 3 Catalyst Copper‐Based Catalysts Cu / Zn O + Element ( Al , Cr , … ) Promotion of Cu / Zn O / MOx Catalysts Cu / Zr O 2 Other Cu , Cu / Me , Cu / Me Ox Catalysts Pd ‐Based Catalysts Sulfide Catalysts Other Catalysts Activation of Cu / Zn Catalyst Activity as a Function of the Nature of Copper‐Based Catalysts Catalyst Deactivation Sintering Sulfur Poisoning Other Poisons By‐Product Formation Reaction Mechanism(s) and Active Sites Cu + in a Zn O Matrix as the Active Center The S chottky Junction Theory Partly Oxidized Copper Independent of Support as Active Sites Metallic Copper in Dynamic Interaction with the Support Cu –Zinc Surface Alloy Model Water Gas Shift Reaction Kinetics Reaction Rate Equations Diffusion Restrictions Kinetics in Slurry Phase Methanol Synthesis Methanol Synthesis Technology Synthesis Gas Preparation Natural Gas Reforming Adiabatic Pre‐Reforming Tubular, Fired Reforming Autothermal Reforming and Oxygen‐Fired Secondary Reforming Gasification of Heavy Oil, Coal or Biomass Coproduction in Ammonia Plants and Use of Off‐gases Economics of Synthesis Gas Preparation Reactor Systems and Synthesis Loop Layout Slurry Phase Reactor Types Methanol Purification Concepts Circumventing the Equilibrium Limitations Other Methanol Synthesis Routes and Technologies Methanol Synthesis by Methane Activation Conclusion

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“…Two other methanol conversion processes are based on systems in which the product methanol is continuously removed from the gas phase by selective adsorption on a solid or in a liquid. The Gas-Solid-Solid Trickle Flow Reactor (GSSTFR) utilizes an adsorbent such as SiO 2 /Al 2 O 3 to trap the product methanol Pass et al 1990). The solid adsorbent is collected in holding tanks and the methanol is desorbed.…”

Section: Reactorsmentioning

confidence: 99%

Integrated Process Configuration for High-Temperature Sulfur Mitigation during Biomass Conversion via Indirect Gasification

Dutta

¹

,

Cheah

²

,

Bain

³

et al. 2012

Ind. Eng. Chem. Res.

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amount of design data, more analysis should be performed for mixed alcohols synthesis to examine biomass-optimized configurations including recycle for maximum conversion and the resulting economics. All biomass fuels have potential to significantly reduce the import of petroleum products. Additionally, economies of scale can play a large factor in lowering the product cost. Therefore, opportunities to co-feed with coal or natural gas systems may be one way to get renewable fuels into the marketplace, just as co-firing biomass with coal is being done in the power generation industry. The impetus for this extensive literature review is the recent reorganization of the U.S. Department of Energy's Office of Energy Efficiency and Renewable Energy (EERE) into eleven new Program Offices. EERE's mission is to strengthen US energy security, environmental quality, and economic health. The Office of Biomass Program is one of these newly created offices. Its goal is developing technologies to transform our abundant biomass resources into clean, affordable, and domestically-produced biofuels, biopower, and high-value bioproducts resulting in economic development, energy supply options, and energy security. In this context, commercially available and nearcommercial syngas conversion processes were evaluated on technological, environmental, and economic bases. This report serves as a first step. Additional, more detailed analyses are required to identify promising, cost-effective fuel synthesis technologies where biomass thermochemical conversion could make an impact. iii Table 1: Summary of Product Information-Facts, Advantages, & Disadvantages Product Facts Advantages Disadvantages H 2 Largest use of syngas Predominately made via SMR Appears to be the most cost competitive option for biomass Automakers working on H 2 fueled vehicles Table of Contents Executive Summary/Conclusions .

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“…The highest production rates were achieved by Frank and Mednick (1982) due to higher catalyst loadings and higher pressure. Figure 34 compares the change in methanol production rate with space velocity at 523 K and 5.2 MPa, and H2/(CO+CO2) of 1 to data by (Pass ,1990) who used the same type of catalyst as that used in this study. Both studies were conducted in a slurry reactor at 523 K. Pass' study was carried out in a 0.3 liter autoclave with catalyst loading of 23 %.…”

Section: Comparison With Other Studiesmentioning

confidence: 99%

A kinetic study of methanol synthesis in a slurry reactor using a CuO/ZnO/Al sub 2 O sub 3 catalyst

Al‐Adwani¹

1992

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A kinetic model that describes the methanol production rate over a CuO/ZnO/A120 3 catalyst (United Catalyst L-951) at typical industrial operating conditions is developed using a slurry reactor. Different experiments are conducted in which the H2/(CO+CO2) ratio is equal to 2, 1, and 0.5, respectively, while the CO/CO 2 ratio is held constant at 9. At each H2/(CO+CO2) ratio the space velocity is set at four different values in the range of 3 000-13 000 1/hr kgca t. The effect of H2/(CO+CO2) ratio and space velocity on methanol production rate, conversions, and product composition is farther investigated. The results indicate that the highest methanol production rate can be achieved at H2/(CO+CO2) ratio of 1 followed by H2/(CO+CO2) ratio of 0.5 and 2 respectively. The hydrogen and carbon monoxide conversions decrease with increasing space velocity for ali H2/(CO+CO2) ratios tested. Carbon monoxide hydrogenation appears to be the main route to methanol at H2/(CO+CO2) ratio of 0.5 and 2. On the other hand, carbon dioxide hydrogenation appears to be the main route to methanol at H2/(CO+CO2) ratio of 1. At all H2/(CO+CO2) ratios, the extent of the reverse water gas shift reaction decreases with increasing space velocity. The effect of temperature on the kinetics is examined by using the same experimental approach at 508 K. It is found that a different reaction sequence takes piace at each temperature.

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Methanol synthesis in a trickle‐bed reactor

Cited by 27 publications

References 24 publications

Methanol Synthesis

Methanol Synthesis

Integrated Process Configuration for High-Temperature Sulfur Mitigation during Biomass Conversion via Indirect Gasification

A kinetic study of methanol synthesis in a slurry reactor using a CuO/ZnO/Al sub 2 O sub 3 catalyst

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