• 한국신재생에너지학회:학술대회논문집
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• 2010.11a
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• pp.131.2-131.2
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• 2010

서부 발전 태안화력발전소에 건설 예정인 IGCC Demo plant의 설계 자료를 근거로 석탄 가스화기의 정상 상태 전산모사를 PRO/II를 사용하여 수행하였다. 석탄을 PRO/II가 받아들일 수 있는 성분으로 바꾼 후 가스화기를 버너와 가스화기 본체의 두 부분으로 나누어 모델링하였다. 버너는 단열조건의 Gibbs Reactor로 모델링하였다. 모사 결과 산소가 완전 소진될 때까지 반응이 진행되는 것을 확인하였다. 가스화기는 char gasification 반응은 kinetic reaction equation으로, gas phase reaction은 equilibrium reactor로 모사하는 알고리듬을 개발 하였으나 PRO/II의 기능에 한계가 있어 간단한 Gibbs Reactor로 모사하였다. 가스화기는 membrane wall에 의하여 냉각되는 것을 고려하여 $1550^{\circ}C$의 균일한 온도에서 반응이 일어나는 것으로 고려하였다. 전산 모사 결과 주요 성분의 조성이 실제 syngas의 조성과 5% 정도 오차가 있는 것으로 나타났다.

• 한국신재생에너지학회:학술대회논문집
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• 2008.10a
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• pp.258-261
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• 2008

상용공정 모사기인 PRO-II를 이용하여 석탄 가스화에 의한 수소 제조공정 개념설계를 수행 하였다. 이 공정은 공기분리(ASU), 석탄가스화, 가스정제, 고온 WGS 반응, 저온 WGS 반응, 수분제거, $H_2$분리, $CO_2$ 분리, $CH_4$ 분리(PSA) 등으로 구성되어 있다. 가스화기의 모사조건은 온도 $1200{\sim}1500^{\circ}C$, 압력 $15{\sim}30atm$, 공급몰비 C:$H_2O$:$O_2$=1:0.5$\sim$1:0.25$\sim$0.5로 하였으며, 정제공정의 온도와 압력은 각각 $550^{\circ}C$, 24.5atm으로 하였다. 생성된 합성가스는 WGS(HTS($400^{\circ}C$, 24atm), LTS($250^{\circ}C$, 23.5atm)) 반응을 거쳐 고순도 수소로 분리정제된다. 석탄을 10ton/day으로 공급하였을 때, 804.0kmol/day의 수소가 생성되었으며, 이때 가스화기 조건은 $1500^{\circ}C$, 25atm, 공급몰비 C:$H_2O$:$O_2$ = 1:0.58:0.43이었다.

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

• Journal of the Korean Institute of Gas
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• v.14 no.5
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• pp.32-37
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• 2010

In this study, vapor-liquid equilibrium (VLE) data at several isothermal temperatures for carbon dioxide and ethane binary systems were estimated using binary interaction parameters (BIP's) in Peng-Robinson (PR) equation of state built-in PRO/II with PROVISION (PRO/II) process simulator. Moreover, BIP's in PR equation of state were newly determined by regressing the experimental VLE data for carbon dioxide and ethane systems for each different isothermal temperatures using the summation of squares of the bubble point deviations as an objective function. Comparative works have been performed for absolute average deviation % (AAD(%)) between experimental and predicted bubble pressures using built-in BIP's in PRO/II and newly regressed one, respectively. Our calculation results gave a better estimation result than the simulation result using an existing parameter built-in PRO/II.

• Journal of the Korea Academia-Industrial cooperation Society
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• v.12 no.7
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• pp.3334-3340
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• 2011

In this study, a computer simulation work has been performed for the carbon dioxide removal process using aqueous amine solution in the GTL (Gas To Liquids) process. 30wt% DEA(diethnaol amine) aqueous solution was utilized as a carbon dioxide remvoal agent and an absorber-stripper two-columns configuration was used. Kent-Eisenburg modeling equation built-in amine specicial package was used for the modeling of the carbon dioxide removal process. PRO/II with PROVISION 9.0, a commercial process simulator was used. Through this simulation study, heat and material balance was obtained and packing column diameter and column height were also estimated.

• Clean Technology
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• v.22 no.4
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• pp.225-231
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• 2016

In this study, modeling and optimization study have been performed to obtain $1,524.58kg\;h^{-1}$ of a solidified NaCl by evaporating a 21.0 wt% of NaCl aqueous solution in order to reduce the steam consumption from $3,139kg\;h^{-1}$ to $496kg\;h^{-1}$ using a two-stage evaporation and a vapor recompression processes. Aspen Plus release 8.8 at AspenTech was utilized for the modeling of two stage evaporation process and PRO/II with PROVISION release 9.4 at Schneider Electric was also used for the simulation of two-stage vapor recompression process with an inter-cooler. For the simulation of the evaporation process containing NaCl aqueous solution, Aspen Plus release 8.8 at AspenTech Inc. was utilized and for the modeling of vapor recompression process PRO/II with PROVISION release at Schneider Electric Inc. For the vapor recompression process, single stage compression and two-stage compression system was compared.

• Journal of the Korean Institute of Gas
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• v.10 no.1 s.30
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• pp.38-42
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• 2006

In this study, a simulation technology for refrigeration cycle which can liquefy and store liquified petroleum gas (LPG) using pure propane as a refrigerant has been introduced. Cooling water as the second cooling medium was used for the liquefaction of propane. Peng-Robinson equation of state was used for the entire refrigeration cycle. A new alpha formulation proposed by Twu et al. was used for the more accurate prediction of vapor pressures of pure propane component and LPG constituents. API method for the accurate estimation of liquid densities of propane and LPG was used instead of using Peng-Robinson equation of state. PRO/II with PROVISION release 7.1, a general purpose chemical process simulator was used for the simulation of the overall refrigeration system. Through this work, we can successfully simulate the real propane refrigeration plant operating at domestic site.

• Journal of the Korea Academia-Industrial cooperation Society
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• v.10 no.12
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• pp.3755-3760
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• 2009

In this study, we have completed the simulation and optimization work for the deethanizer column which was used for natural gas processing plant or saturated gas plant in a petrochemical process. An optimal feed stage location which minimizes the reboiler heat duty was determined. For the modeling of deethanizer, PRO/II with PROVISION was used and Soave modified Redlich-Kwong equation of state model was selected. Through this study, we have found that the minimum number of stage and minimum reflux ratio for separation were 9.03 and 0.62437, respectively and the theoretical stage number was 12, optimal feed stage location was 9 and minimum reboiler heat duty was $12.7470{\times}10^6\;KJ/hr$.

• Korean Chemical Engineering Research
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• v.43 no.4
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• pp.474-481
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• 2005

In this study, modeling and optimization work were performed to obtain nearly pure anhydrous ethanol from aqueous ethanol mixtures using benzene as an entrainer. NRTL liquid activity coefficient model was adopted for phase equilibrium calculations and PRO/II with PROVISION 6.01, a commercial process simulator, was used to simulate the azeotropic distillation process. We used the total reboiler heat duties as an objective function and the concentration of ethanol at concentrator top as a manipulated variable. As a result, 76 mole percent of ethanol at concentrator top gave an optimum value which minimized the total reboiler heat duties of three distillation columns.

• Journal of the Korea Academia-Industrial cooperation Society
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• v.10 no.11
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• pp.3253-3259
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• 2009

In this study, a computer simulation has been performed for the refrigeration cycle using mixed refrigerants in order to decrease the process stream temperature to $-20^{\circ}C$. Refrigerant supply temperature was assumed to be $-30^{\circ}C$ considering the temperature difference as $10^{\circ}C$ with process stream. Peng-Robinson equation of state model was selected for the computer simulation. A new alpha function proposed by Twu et al was used for an accurate prediction of pure component vapor pressure experimental data. One fluid mixing rules were used for the estimation of mixture vapor-liquid equilibria calculations. A commercial process simulator, PRO/II with PROVISION was utilized for the simulation of the overall refrigeration process. In order to minimize the compressor power consumption, we have optimized the two-stage compression system by varying the first stage compressor outlet pressure. Finally, we could obtain the minimum total power 755.7kW at the first stage compressor outlet pressure, 6 bar.