Palghat A., Kinetics Study of Direct Dimethyl Ether Synthesis, IChE International Conference 2011, Hatyai, Thailand, (2011). Kinetics of dehydration of methanol to DME on γ- Al 2O 3 catalyst could be represented as a first order reaction with an activation energy Ea of 256.6 kJ/mol and a frequency factor k o of 8♱0 +28. A stable conversion of methanol of 72% was obtained on g-Al 2O 3 catalyst for the on-stream time of 6 to 10 hour. It was found that g-Al 2O 3 catalyst had a better activity than the two commercial catalysts. Methanol concentration in the influent of the reactor was 0.02 mol/L, 0.05 or 0.07 mol/L. Although DME can be produced easily by the dehydration of methanol, a direct process for integrated production began to be researched in Europe, the U.S. The γ-Al 2O 3 catalyst had a surface area of 194.4 m 2/gram, an average pore diameter of 11.2 nm, and a total pore volume of 0.546 mL/gram. g-Al 2O 3 (from our laboratory), and two commercial catalysts namely catalyst A and catalyst B. The experiment was conducted in a tubular reactor with a diameter of 20 mm. Experiments on dehydration of methanol to produce DME were carried out at a atmospheric pressure (1 bar) and a temperature of 240☌. Burning of DME may produce a cleaner flue gas than LPG. The temperature exotherm occurring in the reactor of 118C. DME may be liquefied at a pressure of about 6 atm (25☌), or a temperature of -25☌ (1 bar). The design given in Figure B.1 uses a single packed bed of catalyst, which operates adia- batically. We performed environmental and economic analyses, and propose the development of a poly-generation process based on economic considerations.A research on the production of dimethyl ether (DME) at lower pressure has been conducted in related to the national program on the partial substitution of LPG with DME in the near future ( RUEN 2017). The DME yield in this study was 0.37, assuming that the DME selectivity was 0.91 and that CO was totally converted. However, the high level of cold energy consumption was a problem during the purification process. Syngas still contained trace amounts of H(2)S and about 3% CO(2) after purification, which satisfied the synthesis demands. The syngas H(2)/CO ratio after water gas shift process was modulated to 1, and the syngas was then purified to remove H(2)S and CO(2), using the Rectisol process. We analyzed the influence of the oxygen/biomass and steam/biomass ratios on biomass gasification and synthesis performance. The whole process comprised four parts: gasification, water gas shift reaction, gas purification, and single-step DME synthesis. In this study, we simulated the single-step process of dimethyl ether (DME) synthesis via biomass gasification using ASPEN Plus. The direct synthesis of dimethyl ether (DME) is an ideal process to achieve the environmental objective of CO2 conversion together with the economic.
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