• Proceedings of the Materials Research Society of Korea Conference
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• 2003.11a
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• pp.239-239
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• 2003

탄소재료의 산화반응을 설명한 대부분의 논문은 TGA(Thermo Gravimetric Analysis)를 이용한 연구이다. TGA 장치는 가열이 필요한 물질의 반응연구에 다양하게 이용되고 있는데, 온도에 대한 무게 변화를 간편하게 알 수 있다는 장점과 함께 보편적으로 편리한 Arrhenius형태의 속도식으로 해석된다. 많은 연구자들은 TGA를 이용하여 다양한 탄소재료에 대한 반응속도상수를 구하였으며, 반응기체, 반응온도 및 원료물질에 따라 다른 속도를 나타내는 실험결과를 표준화된 속도식으로 표현하고자 하는 노력이 있었다. 그러나 이런 대부분의 연구는 coal 등과 같은 탄소재료의 연소특성을 이용하려는 에너지 변환 연구가 주를 이루어 왔으며, 탄소섬유의 산화반응에 대한 표준화 식으로 해석한 보고는 거의 없는 실정이다. 이 연구에서는 내부구조가 현격하게 차이나는 다른 두 종류의 피치계 탄소섬유를 TGA를 이용하여 등온 산화반응 시켰다. 반응기체의 종류와 반응온도를 변화시켜 산화반응조건에 따른 중량변화를 관찰하였고, 여러 산화조건에서 얻어진 산화속도를 Kasaoka 등에 의해 제안된 표준화식을 이용하여 산화반응의 평균 속도상수 K와 전환율이 0.5일 때의 속도상수 $k_{f=0.5}$ 결과를 비교하여 산화 반응속도를 정량적으로 해석하고자 하였다.다.

• Korean Chemical Engineering Research
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• v.50 no.2
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• pp.358-364
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• 2012

The kinetics of the Fischer-Tropsch synthesis and water gas shift reactions over a precipitated iron catalyst were studied in a 5 channel fixed-bed reactor. Experimental conditions were changed as follows: synthesis gas $H_2$/CO feed ratios of 0.5~2, reactants flow rate of 60~80 ml/min, and reaction temperature of $255{\sim}275^{\circ}C$ at a constant pressure of 1.5 MPa. The reaction rate of Fischer-Tropsch synthesis was calculated from Eley-Rideal mechanism in which the rate-determining step was the formation of the monomer species (methylene) by hydrogenation of associatively adsorbed CO. Whereas water gas shift reaction rate was determined by the formation of a formate intermediate species as the rate-determining step. As a result, the reaction rates of Fischer-Tropsch synthesis for the hydrocarbon formation and water gas shift for the $CO_2$ production were in good agreement with the experimental values, respectively. Therefore, the reaction rates ($r_{FT}$, $r_{WGS}$, $-r_{CO}$) derived from the reaction mechanisms showed good agreement both with experimental values and with some kinetic models from literature.

• Electrical & Electronic Materials
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• v.4 no.4
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• pp.344-353
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• 1991

무정형 SiC 박막을 수평형 CVD반응기로부터 SiH$_{4}$ 및 H$_{2}$를 반응기체로 하여 실리콘 웨이퍼위에 증착시켜 제조하였다. 박막 성장 속도는 상압에서 650.deg.C와 850.deg.C범위에서 측정되었다. 반응기체의 유량은 1000sccm으로 고정하였으며 SiH$_{4}$와 CH$_{4}$의 유량을 변화시켰다. 증착 반응속도식으로 표면 반응이 율속단계인 Eley-Rideal 모델과 SiH$_{4}$와 CH$_{4}$의 종도에 m차로 비례하는 두가지 속도식을 가정하였다. 증착시간에 따른 SiC 박막두께의 측정으로부터 얻은 증착 반응 속도로부터 회귀 분석법에 의하여 두가지 반응속도식의 반응속도 상수를 구하였다. 얻어진 반응속도식에 의해서 계산된 값과 실험치를 비교한 결과 0.15차의 반응속도식이 Eley-Rideal반응기구보다 약산 더 잘 맞음을 알 수 있으나 두 모델 다 약간씩 실험결과와 차이가 나고 있다. 이것은 본 실험의 증착 조건의 율속단계가 확산 단계와 표면 반응 단계의 전이영역 즉 본 실험의 증착조건에서 확산속도와 표면 반응속도가 비슷하기 때문으로 생각된다. 또한 Eley-Rideal 반응기구에서 부터 얻어진 SiH$_{4}$ 및 CH$_{4}$의 흡착평형상수 $K_{s}$ 와 $K_{c}$ 값을 비교하면 1000K이하에서는 $K_{s}$ 가 $K_{c}$ 보다 큰 값을 가지는데 이것은 Gibbs 자유에너지 최소화 방법에서 구한 결과와 일치하였다.

• Journal of the Korean Chemical Society
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• v.52 no.3
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• pp.217-222
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• 2008

We investigate the kinetics of diffusion-influenced catalytic reactions occurring in small reaction volume. From a simple exact model study, we find that the reaction rate coefficient decreases with the size of reaction volume. The explicit expression for the average reaction rate constant is presented, which can be regarded as a generalization of well-known Collins-Kimball rate constant into the reactions occurring in a small reaction volume. It turns out that the traditional diffusion influenced reaction dynamics is followed by a single exponential relaxation phase with a rate constant dependent on the reaction volume for the catalytic reactions occurring in small reaction volumes.

• Clean Technology
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• v.19 no.1
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• pp.51-58
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• 2013

In this study, kinetics data was obtained for steam reforming reaction of ethane over the nickel catalyst. The variables of steam reforming reaction were reaction temperature, partial pressure of ethane, and mole ratio of steam and ethane. Parameters for the power rate law kinetic model and the Langmuir-Hinshelwood model were obtained from the kinetic data. Also, sizing of steam reforming reactor was performed by using PRO/II simulator. For the steam reforming reaction of ethane, Langmuir-Hinshelwood model determining the reaction rate by the surface reaction was better suited than a simple power rate law kinetic model. On water-gas-shift reaction, power rate law kinetic model was well fitted to the kinetic data. Reactor size can be calculated for production of hydrogen through PRO/II simulation.

• Journal of the Korean Chemical Society
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• v.51 no.4
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• pp.365-374
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• 2007

The purpose of this study is to investigate the students' conceptions about the reaction rate changes during the chemical equilibrium shifts and also whether the questions about basic concepts of the reaction rate are helpful for the students' understanding of reaction rate changes during the chemical equilibrium shifts. The subjects were 100 students in the 12th grade. The questionnaires were composed of A, B, and A' set, which had to be answered sequentially. The A set consisted of questions asking the change of reaction rate when chemical equilibrium was shifted, the B set was to testify the basic concepts of the reaction rate, and the A' set was the same as the A set. The results showed that the students' understanding of the reverse reaction rate change was lower than that of the forward reaction rate change during the equilibrium shift. Also it was found that students' understanding of the reaction rate change caused by adding the reactant was fairly good while their understanding of the reaction rate change caused by temperature increment was very poor. Since the students marked very high scores in the B set questions, their poor understanding for the reaction rate changes during the equilibrium shifts was not seemed to be due to the lacks of the basic knowledge of reaction rate. Instead, it was due to the failure of applying the basic knowledge of reaction rate to the changes of reaction conditions. It was also found that the average scores of A' set were statistically higher than those of A set. It means the B set items were helpful for the students to solve the A' set items. These results evidenced the possibility of set questionnaires could help the students to connect the related concepts in solving the problems.

• Proceedings of the Korean Environmental Sciences Society Conference
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• 2006.11a
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• pp.469-472
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• 2006

BI 및 ETABr의 농도변화에 따른 속도상수의 변화는 이 반응이 단순한 1차 및 2차 반응 속도식에 맞지 않는다. 이와 같은 현상은 용액 속에서 두 반응 시약인 p-NPDPIN 및 BI와 상전이촉매인 ETABr 사이에 많은 수의 작은 응집된 입자(aggregates)을 형성함을 의미한다. 수용액 속에서는 불용성인 p-NPDPIN과 수용성인 BI가 충돌하여 반응할 기회가 적은데 반하여 ETABr은 이 두 시약을 함께 수용하여 세 분자 사이에 응집현상이 일어남으로 p-NPDPIN과 BI가 반응하기에 충분한 거리 내에 있게 된다. 바꾸어 말하면, 이 두 반응물질이 1:1 adducts로 반응하기보다는 여러 ETABr과 함께 많은 수의 반응분자들이 회합(응집) 되어 있음을 뜻한다.

• Journal of Soil and Groundwater Environment
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• v.9 no.2
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• pp.20-27
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• 2004

Kinetic characteristics dependent on several factors such as iron mineral and organic solvents were investigated. When F $e^{0}$ , FeS and Fe $S_2$ were used as mediators, minerals affecting reaction rate were in the following order : $Fe_{0}$ 0/ ＞ FeS ＞ $FeS_2$ when in contact $C_2$C $l_{6}$ . The more chloride substituted, the higher reaction rate were observed. The reaction rates were dependent on pH, shaking rate, temperature and specific surface area. 1, 10-phenanthroline and EDTA degradation rates were fast, indicating that they adsorbed on the surface of the iron which makes the electron transfer reaction easy. Nitrate which has $\pi$＊ orbital of molecular can increase electron transfer rate because it is delocalized in its entity. The reaction rates were not affected by hydroquinone. Degradation rates were much enhanced with naturally occurring kaolinite because of the surface corrosion of Fe mineral. However, The reaction rate was not affected by F $e^{2+}$ or S $O_4$$^{2-}$ presented in solution.n.

• Proceedings of the Materials Research Society of Korea Conference
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• 2003.11a
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• pp.240-240
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• 2003

탄소재료의 가스화속도는 근본적으로 활성자리의 수와 관련되어 있으며, 또한 가스화속도는 활성자리 뿐 아니라 확산제한에 따라 달라진다. 대부분의 탄소재료의 활성화 초기단계는 제한된 활성자리 때문에 반응속도는 느리고, 다음 단계는 총 활성자리가 증가하여 반응속도는 급격히 증가하고, 마지막으로 활성자리가 감소하여 활성화 속도는 감소한다. 이러한 sigmoidal특성을 나타내는 활성화 단계를 기공발달과정으로 설명하면, 활성화 초기에 탄소재료 내부에 이미 존재하는 닫힌 기공이 열리고, 일단 기공이 열리면 성장하게 된다. 이렇게 기공 수가 증가하는 것 뿐 아니라 기공 직경이 증가하여 활성화 과정이 진행될수록 비 표면적 및 기공부피는 증가하는데 이런 일련의 과정을 통하여 활성자리 수는 증가하고 또는 감소한다. 이렇게 기공이 발달하는 과정은 각각의 활성화 단계에서 탄소재료의 비 표면적 측정으로 알 수 있으며, 전반적인 산화속도 변화를 측정하여 반응단계를 추정하게 된다. 대부분의 연구자들은 반응 전체의 평균 산화속도를 측정한 후 활성화 에너지를 구하여 반응조절단계로 활성화 기구를 설명한다. 이 연구에서는 활성화 과정 중에 발생하는 중량감소 단계, 즉 각각의 활성화 단계에 따라 달라지는 반응속도상수를 측정하고, 반응단계별 활성화 에너지를 비교 해석하여 피치계 탄소섬유의 기공발달에 영향을 미치는 활성화 기구를 고찰하고자 하였다.

• The Journal of Engineering Research
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• v.3 no.1
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• pp.223-233
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• 1998

The kinetic and mechanism of the hydrothermal reaction between lime and quartz used solid state reaction equations have been investigated. Hydrothermal reaction on the starting materials was carried out in an autoclave that quartz mixed with calcium hydroxide in CaO/$SiO_2$ ratio of 0.8-1.0 for 0.5-8 hour at saturated steam pressure of $180-200^{\circ}C$. The rate of reaction was given from the ratio of uncombined lime and quartz content to the total lime and quartz content. The rate of reaction was obtained the results by the Jander's equation $[1-(1-\alpha)^{1/3}]^N=Kt$. The reaction of lime is controlled mainly by the dissolution such as N=1, and the reaction of quartz is controlled mostly by the diffusion such as $N\risingdotseq2$. The rate of hydrothermal reaction in the calcium silicate hydrates system is suggested to be determined generally by the mass transfer through the product laver formed around the reactant particles. The rate equation for whole hydrothermal reaction is shown that it is converted into the rate determining step by the diffusion from the boundary reaction such as approximately $N=1-2$.