• 한국가스학회:학술대회논문집
• /
• 2005.10a
• /
• pp.141-145
• /
• 2005

DME (Di-Methyl Ether) is a new clean fuel and an environmental-friendly energy resource, also is recently increasing with an alternative interest because of the industrial use. DME has been shown to have excellent properties as a diesel fuel giving emission level better than ULEV standard. So it has been attracting considerable as an alternative diesel fuel. In this study, we carried out simulation of separation and purification process of demo plant for 101on per day DME production, which cause the effect that is important in productivity, from operation results of pilot plant for 50kg per day DME production. The liquefied stream, which was separated by gas-liquid separator after DME reactor, includes $CO_2$, DME, Methanol and $H_2O$. We established three distillation columns for separation and purification of the stream. $CO_2$ was extracted from the stream by first distillation column, DME was extracted by second column and Methanol was extracted by third column. We investigated and analyzed the effect which the actual operation variables cause in efficiency of process and optimized process, finally we got the DME of purity $100\%$.

• Korean Chemical Engineering Research
• /
• v.52 no.6
• /
• pp.796-806
• /
• 2014

The key for the commercial deployment of IGCC power plants or chemical (methanol, dimethyl ether, etc.) production plants based on coal gasification is their economic advantage over plants producing electricity or chemicals from crude oil or natural gas. The better economy of coal gasification based plants can be obtained by co-production of electricity and chemicals. In this study, we carried out the economic feasibility analysis on the process of co-producing electricity and DME (dimethyl ether) using coal gasification. The plant's capacity was 250 MW electric and DME production of 300,000 ton per year. Assuming that the sales price of DME is 500,000 won/ton, the production cost of electricity is in the range of 33~58% of 150.69 won/kwh which is the average of SMP (system marginal price) in 2013, Korea. At present, the sales price of DME in China is approximately 900,000 won/ton. Therefore, there are more potential for lowering the price of co-produced electricity when comparing that from IGCC only. Since the co-production system can not only use the coal gasifier and the gas purification process as a common facility but also can control production rates of electricity and DME depending on the market demand, the production cost of electricity and DME can be significantly reduced compared to the process of producing electricity or DME separately.

• Journal of the Korean Institute of Gas
• /
• v.10 no.2 s.31
• /
• pp.22-26
• /
• 2006

In this study, modeling and simulation works using Aspen Plus were carried out for DME separation and purification process of pilot plant for the daily production of 50 kg of DME. For modeling of the entire DME separation unit, NRTL liquid activity coefficient model was used for the prediction of liquid phase non-idealities, Henry's law option was also used for the estimation of solubilities of light gases in solvents and SRK equation of state model was utilized for the description of vapor phase non-idealities. DME having over 98 wt% purity was obtained as a side distillate product in a DME purification column.

• Transactions of the Korean hydrogen and new energy society
• /
• v.22 no.6
• /
• pp.925-933
• /
• 2011

The traditional feedstock for dimethyl ether (DME) has been natural gas obtained by pipeline from a nearby natural gas or oil field. This report focuses on other feedstock: Coal bed methane (CBM). The resource availability and suitability of CBM for DME manufacturing have been investigated. CBM in a short time has become an important industry, providing an abundant clean-burning fuel and also suggesting as a feedstock for gas industry. The use of CBM will have very little impact on the KOGAS' DME process design and economics up to 50 vol% of $CO_2$ in the CBM source. Many of the CBM sources in Asia are high in $CO_2$, but pose no difficulties for the KOGAS' DME plant. Since tri-reformer requires substantial $CO_2$ in its feed, no $CO_2$ removal from the CBM feed is needed. The $CO_2$ in the CBM means that less $CO_2$ needs to be recycled from the downstream in the process.

• Clean Technology
• /
• v.23 no.3
• /
• pp.237-247
• /
• 2017

In the dimethyl ether (DME) synthesis and separation process, over 8% by mole of $CO_2$ is fed to the DME synthesis reactor which lowers DME productivity. Therefore, this work focused on the removal of $CO_2$ using three kinds of processes with physical absorbents by comparing the utility consumption through computer simulation of each process. Among the processes selected for comparison are Rectisol$^{(R)}$ process using methanol, Purisol$^{(R)}$ process using n-methyl pyrrolidone (NMP), and SelexolTM process using dimethyl ethers of polyethylene glycol (DEPG) as a solvent. As a result of this study, it was concluded that Purisol$^{(R)}$ process consumes the least energy followed by SelexolTM process. Therefore, it is considered that Purisol$^{(R)}$ process is the most suitable method to absorb $CO_2$ contained in the feed of DME synthesis reactor.

• Journal of the Korea Academia-Industrial cooperation Society
• /
• v.15 no.7
• /
• pp.4698-4706
• /
• 2014

In this study, the simulation was performed for the CO removal process using a composite membrane in DME production. The composite membrane, PEI-PDMS (polyetherimide- polydimethyl siloxane) manufactured by Airrane Co. Ltd., was used in the modeling through a commercial simulation design program, PRO/II with PROVISION 9.2 by Invensys. To simulate the process, the permeability constants of each of the pure component from Airrane Co. Ltd. were determined by regression analysis from the experimental data. The required separation membrane area and utility cost in the CO removal process were obtained using a chemical process simulator and composite membrane with a compatible permeability constant.

• Transactions of the Korean hydrogen and new energy society
• /
• v.25 no.1
• /
• pp.79-86
• /
• 2014

In Dimethyl Ether (DME) indirect production processes, DME have a reforming process to separate Methanol. DME has a high cetane number and Methanol has a high octane number. Each fuel has a different combustion characteristics and reactivity. So, this paper was investigated on the combustion characterisitics of DME and Methanol. Basically, Methanol has a effect of retarding ignition. However, Within 10% of total carbon mole number in DME, Methanol slightly changed the onset timing of Low Temperature Reaction (LTR) with increasing thermal-ignition preparation range. It means that controlling combustion phasing of DME can be possible without eliminated LTR. In case of IMEP, the ranges.

• Clean Technology
• /
• v.18 no.4
• /
• pp.347-354
• /
• 2012

In this study, simulation works have been performed for the $CO_2$ removal process contained in the DME production process using NMP (N-methyl-2-pyrrolidone) as a solvent. PRO/II with PROVISION release 9.1 at Invensys was used as a chemical process simulator and NRTL activity coefficient model with Henry's law option and Soave-Redlich-Kwong equation of state were used for thermodynamic models. For the determination of the binary interaction parameters in NRTL model, regression works have been performed to match the experimental thermodynamic data. Optimal feed tray location which minimizes the reboiler heat duty was determined.

• 한국가스학회:학술대회논문집
• /
• 2005.05a
• /
• pp.232-232
• /
• 2005

• Journal of the Korea Academia-Industrial cooperation Society
• /
• v.14 no.3
• /
• pp.1502-1511
• /
• 2013

In this study, simulation works have been performed for the modeling of $CO_2$ removal process contained in the DME production process through an absorber-stripper system using methanol aqueous solution. Aspen Plus release 7.3 in AspenTech company was utilized as a simulation tool and PC-SAFT modeling equation of state was used as a thermodynamic model. Fitting parameters built-in PC-SAFT model was determined by regressing experimental data, predicted results using PC-SAFT model were compared with experimental data in order to verify the exactness of the thermodynamic model. Optimization works have been performed to reduce the utility consumptions using solvent circulation rate, column operating pressure and feed stage location as manipulated variables.