From laboratory experiments to simulation studies of methanol dehydration to produce dimethyl ether reaction—Part II: Simulation and cost estimation

Efficient Methanol Dehydration to DME and Light Hydrocarbons by Submicrometric ZrO2-ZSM-5 Fibrillar Catalysts with a Shell-Like Structure

“…The calculated preexponential factor and activation energy values were 3.9•10 4 molMeOH•gZSM-5 -1 •s -1 •atm -1 and 75 kJ/mol, respectively. The value of activation energy calculated in the present work is in good agreement with other studies available in the literature, dealing with methanol dehydration to DME using zeolite catalysts, which reported values for this kinetic parameter ranging from 52-61 kJ/mol [40,62,63] to 90-100 kJ/mol [64][65][66]. The presence of acid sites with a high strength on the surface of ZSM-5 zeolite, further promotes DME dehydration to hydrocarbons [67,68].…”

A Review on Deactivation and Regeneration of Catalysts for Dimethyl Ether Synthesis

“…In Table 1, selected catalysts, process parameters of DME synthesis, and reasons for deactivation are presented. A fixed-bed reactor system is the most often used on a laboratory scale or in pilot plants due to the low production costs and simplicity [100]. In this type of reactor, the diffusion limitations are eliminated through gas-solid contact.…”

“…Studies have shown that the thermal sintering process, in the case of a copper-based catalyst, is kinetically slow and hardly reversible or completely irreversible; however, it can be prevented by controlling the process temperature. Consequently, a high synthesis gas recycling rate is required to avoid temperature rises, with consequent lower conversion and ultimately high operating costs [1,100]. An alternative to synthesis gas comprising H 2 and CO is the use of CO 2 instead of CO.…”

Techno‐Economic Analysis of the Carbon Dioxide (CO2)–Ethane Azeotrope Separation for Natural Gas Processes

“…To make ab este valuation, the equipment costs of the precooling and conventional systems are estimated by using the procedures proposed by Douglas and the other researchers. [14][15][16][17][18][19]…”

“…in which Q con (W) is the condenser load, U con is the overall heat-transfer coefficient, and the log-mean temperature driving force DT cond (K) dependso nt he dew and bubblep oints for at otal condenser. [19] Capital investment ¼column cost þ tray cost þtotal heat exchanger cost ð12Þ…”