A novel distillation design for vapor phase dimethyl ether production process

2013 ◽  
Vol 9 (3) ◽  
pp. 464-470
Author(s):  
Yadollah Tavan ◽  
Mohammad Reza Khosravi Nikou
Keyword(s):  
Production Process ◽  
Dimethyl Ether ◽  
Vapor Phase ◽  
Distillation Design

Vapor phase carbonylation of dimethyl ether and methyl acetate with nickel-active carbon catalysts

1983 ◽  
Vol 7 (3) ◽  
pp. 361-368 ◽  
Author(s):  
Tsutomu Shikada ◽  
Kaoru Fujimoto ◽  
Michiharu Miyauchi ◽  
Hiro-o Tominaga
Keyword(s):  
Dimethyl Ether ◽  
Vapor Phase ◽  
Active Carbon ◽  
Methyl Acetate ◽  
Carbon Catalysts

VAPOR PHASE CARBONYLATION OF METHYL ACETATE, METHANOL, AND DIMETHYL ETHER WITH MOLYBDENUM-ACTIVE CARBON CATALYST

1985 ◽  
Vol 14 (4) ◽  
pp. 547-550 ◽  
Author(s):  
Tsutomu Shikada ◽  
Hiroshi Yagita ◽  
Kaoru Fujimoto ◽  
Hiro-o Tominaga
Keyword(s):  
Dimethyl Ether ◽  
Vapor Phase ◽  
Active Carbon ◽  
Methyl Acetate ◽  
Carbon Catalyst

scholarly journals Process simulation of dimethyl ether synthesis via methanol vapor phase dehydration

2013 ◽  
Vol 15 (2) ◽  
pp. 122-127 ◽  
Author(s):  
Ziyang Bai ◽  
Hongfang Ma ◽  
Haitao Zhang ◽  
Weiyong Ying ◽  
Dingye Fang
Keyword(s):  
Dimethyl Ether ◽  
Vapor Phase ◽  
Process Simulation ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Reflux Ratio ◽  
Methanol Vapor ◽  
Operation Conditions ◽  
Dimethyl Ether Synthesis ◽  
Simulation Results

The production processes included catalytic dehydration of methanol in an adiabatic fixed-bed reactor and two columns product separations. In this study, the technological process for dimethyl ether (DME) synthesis is built on PRO/II platform based on the combined parameters of the reaction dynamic model for methanol dehydration reaction, the improved NRTL model of the liquid phase, the PR model of vapor phase. In order to validate the proposed model, the simulation results have been compared with the available data from a set of industrial production equipment with a production capacity of 200 000 tonnes per annum. A comparison between the calculated and measured results has proved that these results are satisfactory. The bed height and the volume of the catalytic bed are calculated aim at one million t/a DME yields and while taking account of high-purity DME production. After discussing the influence of feed stage location and reflux ratio for DME product purity, the suitable unit operation conditions are chosen. Accordingly, accurate process simulation results provide the basis and guidance for an improvement and development of the similar industrial device.

Dimethyl Ether as an Additive to Steam for Improved Steam-Assisted Gravity Drainage

SPE Journal ◽  
2018 ◽  
Vol 23 (04) ◽  
pp. 1201-1222 ◽  
Author(s):  
Kai Sheng ◽  
Ryosuke Okuno ◽  
Mingyuan Wang
Keyword(s):  
Dimethyl Ether ◽  
Vapor Phase ◽  
Carbon Number ◽  
Water Soluble ◽  
Gravity Drainage ◽  
Solvent Recovery ◽  
Steam Chamber ◽  
Steam Assisted Gravity Drainage ◽  
Edge Conditions ◽  
Edge Temperature

Summary Coinjection of solvent with steam results in lower chamber-edge temperatures than those in steam-assisted gravity drainage (SAGD), which enables the decrease of heat losses to the overlying formation rocks. However, use of highly volatile solvents, such as propane, can yield significantly slow bitumen production because of low chamber-edge temperatures. The suitability of alkane solvents for SAGD in terms of phase behavior has been reported to increase with increasing carbon number and tends to level off at a certain carbon number, which is approximately C6 for Athabasca bitumen reservoirs. The main objective of this research is to investigate the potential of dimethyl ether (DME), a water-soluble solvent, as an additive to steam for reducing steam/oil ratio (SOR) while keeping SAGD-like rates of bitumen production. The chamber-edge temperature for a given overall composition and operating pressure is defined as the temperature at which the vapor phase completely condenses with decreasing temperature. Thermodynamic predictions show that the chamber-edge temperature so defined will increase substantially if the solvent can partition into the aqueous phase at chamber-edge conditions. This is confirmed in numerical-reservoir simulation for coinjection of steam with DME, as a water-soluble solvent, for Athabasca bitumen. In simulation case studies, coinjection of steam with DME (DME-SAGD) is compared with SAGD and coinjection of steam with C4 (C4-SAGD), in terms of SOR, bitumen production, local displacement efficiency, and solvent recovery. The steam-injection pressure is 35 bar for all cases, and 2 mol% of solvent is coinjected in solvent-SAGD simulations until the steam chamber reaches the side boundary of a 2D homogeneous reservoir model. Because the DME volatility is between C3 and C4, C4 is selected as the alkane counterpart in this simulation study to see the effect of the solvent solubility in water on oil recovery in solvent-SAGD. DME is more volatile and less soluble in bitumen than C4 at their corresponding chamber-edge conditions. However, results show that DME-SAGD results in 35% lower SOR than SAGD while being able to increase bitumen-production rates of SAGD. Analysis of simulation results indicates that the solubility of DME in water not only makes the chamber-edge temperature higher than that of C4-SAGD, but also yields 15% higher solvent-recovery factor than C4-SAGD. The main reason for the latter observation is that a much-smaller fraction of the injected solvent is present in the vapor phase in DME-SAGD than in C4-SAGD. Also, DME dissolves in both water and bitumen, which results in the aqueous and oleic phases of nearly equal density within the gravity-drainage zone near the edge of a steam chamber. This is the neutral regime of oil/water two-phase flow along the chamber edge between the two extreme cases: SAGD and C4-SAGD. Unlike in C4-SAGD, the reduced gravity segregation in DME-SAGD is expected to facilitate the mixing of condensed solvent with bitumen near the edge of a steam chamber.

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