• Resources Recycling
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• v.10 no.2
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• pp.27-33
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• 2001

Reusing of electroless Ni-Cu-P waste solution was investigated in the plating time, plating rate, solution composion and deposit. Plating time of nickel-catalytic surface took longer than that of zincated-catalytic surface. Initial solution with 50f) waste solution additive at batch type was possible to reusing of waste solution. Plating time of initial solution at continuous type took longer 10 times over than that of batch type. Plating time of 50% waste solution additive at continuous type took longer 3.7 times over than that of batch type. Component change of nickel-copper for electroless deposition was greatly affected by depolited inferiority and larger decreased plating rate.

• 한국신재생에너지학회:학술대회논문집
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• 2007.11a
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• pp.97-100
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• 2007

A fluidized bed reactor made of quartz with 0.055 m I.D. and 1.0 m in height was employed for the thermocatalytic decomposition of methane to produce $CO_2$ - free hydrogen . The fluidized bed was proposed for the continuous withdraw of product carbons from the reactor. The methane decomposition rate with the carbon black N330 catalyst was quickly reached a quasi-steady state rate and remained for several hour. The methane and propane mixture decomposition reaction was carried out at the temperature range of 850 - 900 $^{\circ}C$, methane and propane mixture gas velocity of 1.0 $U_{mf}$ ${\sim}$ 3.0 $U_{mf}$ and the operating pressure of 1.0 atm. Effect of operating parameters such as reaction temperature, gas velocity on the reaction rates was investigated. The produced carbon by the methane decomposition was deposited on the surfaces of carbon catalysts and the morphology was observed by TEM image.

• Resources Recycling
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• v.12 no.1
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• pp.18-24
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• 2003

Reusing of electroless Ni-Cu-B waste solution was investigated in the plating time, plating rate, solution composition and deposit. Plating time of nickel-catalytic surface took longer than that of zincated-catalytic surface. Initial solution with 40% waste solution additive at batch type was possible to reusing of waste solution. Plating time of initial solution at continuous type took longer 6 times over than that of batch type. Plating time of 40% waste solution additive at continuous type took longer 2 times over than that of batch type. Component change of nickel-copper for electroless deposition was greatly affected by deposited inferiority and larger decreased plating rate.

• 한국신재생에너지학회:학술대회논문집
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• 2006.06a
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• pp.85-88
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• 2006

A fluidized bed reactor made of quartz with 0.055m I.D. and 1.0m in height was employed for the thermocatalytic decomposition of propane to produce $CO_2$-free hydrogen. The fluidized bed was proposed for the continuous withdraw of product carbons from the reactor. The propane decomposition rate used carbon black N33O as a catalyst. The propane decomposition reaction was carried out at the temperature range of $600{\sim}800^{\circ}C$, paropane gas velocity of $1.0 U_{mf}\;3.0U_{mf}$ and the operating pressure of 1.0 atm. Effect of operating parameters such as reaction temperature, gas velocity on the reaction rates was investigated. The carbon which was by-product of methane decomposition reaction was deposited on the catalyst surface that was observed by SEM. Resulting production in our experiment were not only hydrogen but also several by products such as methane, ethylene, ethane, and propylene.

• Transactions of the Korean hydrogen and new energy society
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• v.22 no.4
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• pp.465-473
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• 2011

To find the optimum mixing ratio of WGS catalyst with $CO_2$ absorbent for SEWGS process, water gas shift reaction tests were carried out in a fluidized bed reactor using commercial WGS catalyst and sand (as a substitute for $CO_2$ absorbent). WGS catalyst content, gas velocity, and steam/CO ratio were considered as experimental variables. CO conversion increased as the catalyst content increased during water gas shift reaction. Variations of the CO conversion with the catalyst content were small at low gas velocity. However, those variations increased at higher gas velocity. Within experimental range of this study, the optimum operating condition(steam/CO ratio=3, gas velocity = 0.03 m/s, catalyst content=10 wt.%) to get high CO conversion and $CO_2$ capture efficiency was confirmed. Moreover, long time water gas shift reaction tests up to 20 hours were carried out for two cases (catalyst content = 10 and 20 wt.%) and we could conclude that the WGS reactivity at those conditions was maintained up to 20 hours.

• Applied Chemistry for Engineering
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• v.4 no.2
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• pp.308-317
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• 1993

The study is related to the synthesis of acrylic acid by selective oxidation of acrolein on Mo-V-W multicomponent mixed oxide catalysts. Mo-V-W-O(WVM), Mo-V-O/Mo-W-O(VM/WM), Mo-W-O/Mo-V-O(WM/VM) and mechanical mixtures of Mo-V-O and Mo-W-O(M-VM+WM) were prepared and characterized by BET, XRD, SEM and EPMA. Catalytic activity of these catalysts was tested in a continuous fixed bed reactor. In WVM catalysts small amount of tungsten added to VM increased surface area and selectivity of acrylic acid, but excess amount of tungsten decreased reaction rate of acrolein and selectivity. VM/WM catalysts, VM supported on WM, showed higher activity and selectivity than WM/VM catalysts where WM is supported on VM. Phase cooperation between WM and VM was observed in mechanical mixture of WM and VM and they showed higher yield than WM or VM.

• Korean Chemical Engineering Research
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• v.45 no.4
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• pp.340-344
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• 2007

Catalytic upgrading of pyrolytic bio-oil produced from Japanes Larch was carried out over MCM-41 catalyst. Oil with enhanced stability was produced by the MCM-41 catalyst due to transform oxygen known as a main cause for the instability of bio-oil into $H_2O$, CO and $CO_2$. In addition, the MCM-41 catalyst produced the larger amount of phenolic compounds in the pyrolytic bio-oil product compared with that in the bio-oil produced without catalyst. Especially, the catalytic activity of Al-MCM-41 for the bio-oil upgrading was higher than that of Si-MCM-41 because Al-MCM-41 has the larger amount of acid sites. Also, the better reforming result was obtained when pyrolytic bio-oil vapor passed through catalytic layer rather than Japanese Larch was mixed with catalyst directly.

• Proceedings of the KAIS Fall Conference
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• 2011.05b
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• pp.854-857
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• 2011

육방정프레스 $420{\phi}$를 활용한 고온고압(high pressure high temperature: HPHT) 방법으로 금속촉매층 ($Ni_{77}Fe_{11}Mn_9Co_3$)과 카본디스크가 순차적으로 적층된 셀에 인산칼슘을 첨가함에 따라 합성다이아몬드 성장에 미치는 변화를 확인하였다. HPHT 공정의 압력, 온도, 시간을 각각 8 GPa, $1500^{\circ}C$, 280s로 고정하고, 카본과 금속촉매 층 사이에 인산칼슘을 각각 0, 0.08, 0.20, 0.28 mg씩 첨가하여 고온고압 합성을 수행하였다. 합성공정 후 적층셀의 중간부 셀 수직단면을 광학현미경과 마이크로 라만분광기로 분석하였다. 결과적으로 인산칼슘을 0.08 mg 도포하여 첨가하면 다이아몬드의 생성이 향상되었다. 반면 0.20 mg 이상에서는 도포되는 양이 증가 할수록 다이아몬드 생성이 억제되다가 0.28 mg 이상 첨가에서는 다이아몬드가 거의 생성되지 않는 특징을 보였다.

• Proceedings of the Korea Society for Energy Engineering kosee Conference
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• 2006.05a
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• pp.244-249
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• 2006

• 한국가스학회:학술대회논문집
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• 2005.05a
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• pp.214-214
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• 2005