• Clean Technology
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• v.24 no.1
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• pp.35-40
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• 2018

$Co_3O_4$ catalysts for $N_2O$ decomposition were prepared by co-precipitation method. Ce and Zr were added during the preparation of the catalyst as promoter with the molar ratio (Ce or Zr) / Co = 0.05. Also, 1 wt% $K_2CO_3$ was doped to the prepared catalyst with impregnation method to investigate the effect of K on the catalyst performance. The prepared catalysts were characterized with SEM, BET, XRD, XPS and $H_2-TPR$. The $Co_3O_4$ catalyst exhibited a spinel crystal phase, and the addition of the promoter increased the specific surface area and reduced the particle and crystal size. It was confirmed that the doping of K improves the catalytic activity by increasing the concentration of $Co^{2+}$ in the catalyst which is an active site for catalytic reaction. The catalytic activity tests were carried out at a GHSV of $45,000h^{-1}$ and a temperature range of $250{\sim}375^{\circ}C$. The K-impregnated $Co_3O_4$ catalyst showed much higher activity than $Co_3O_4$ catalysts with promoter only. It is found that the K-impregnation increased the concentration of $Co^{2+}$ more than the added of promoter did, and lowered the reduction temperature to a great extent.

• Applied Chemistry for Engineering
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• v.17 no.3
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• pp.321-326
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• 2006

Thermal degradation of styrene dimer fraction (SDF, main compound: 47 wt% of 1,3-diphenylpropane), 5~15% of total products produced during decomposition of waste expanded polystyrene (WEPS) was investigated. Reaction condition of $360^{\circ}C$, and 152 kPa to 202 kPa was an optimum for high pressure degradation. Under this operating condition, the yield of oil was 73.8% and the selectivities to Ben, Tol, EB, SM, and AMS were 0.4, 30.9, 15.0, 19.6, and 4.2%, respectively. Non-catalytic fixed bed continuous degradation was conducted at reaction temperatures of $510{\sim}610^{\circ}C$ and contact time ranges of 2~24 min, where the yield was increased by increasing of reaction temperature and contact time. A $Cr_2O_3$ catalyst showed the highest activity and SM yield among acid, base, and redox catalysts. The conversion of 74.6% and the yield of Ben, Tol, EB, SM, and AMS were 0.4, 21.6, 9.7, 17.9, and 3.5%, respectively at $560^{\circ}C$ and contact time of 24 min. It is thought that styrene is converted to EB and other secondary products throughout the formation of diradicals of styrene.

• Korean Chemical Engineering Research
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• v.46 no.1
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• pp.82-87
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• 2008

$N_2O$ decomposition characteristics of dual bed mixed metal oxide catalytic system was investigated. The partial oxidation of methane at first reactor of dual bed catalytic system was performed over Co-Rh-Al (1/0.2/1) catalyst under the optimized condition of $8,000h^{-1}$ GHSV, gas ratio ($CH_4:O_2=5:1$) at $500^{\circ}C$. In the dual bed system investigated herein, the second catalyst bed was employed for the $N_2O$ decomposition using product of partial oxidation of methane at first bed. An excellent $N_2O$ conversion activity even at lower temperature ($<250^{\circ}C$) was obtained with Co-Rh-Al (1/0.2/1) or Co-Rh-Zr-Al (1/0.2/0.3/1) catalyst by combining Co-Rh-Al (1/0.2/1) hydrotalcite catalyst for the partial oxidation of methane in a dual-bed system. The $N_2O$ conversion activity is drastically reduced in the presence of oxygen in second bed of a dual-bed system over Co-Rh-Al (1/0.2/1) catalyst at $300^{\circ}C$.

• Journal of Korean Society of Environmental Engineers
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• v.37 no.12
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• pp.668-673
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• 2015

Alumina-based catalysts with different Ce loadings were studied in the decomposition of $CF_4$ using microwave heating system. Heating material of microwave system used Silicon Carbide. The crystallographic phases of catalysts were investigated by XRD and decomposition rates of $CF_4$ were examined by GC-TCD. The catalysts of 10 wt% Ce modified $Al_2O_3$ showed higher $CF_4$ decomposition rate than un-modified $Al_2O_3$ for $500^{\circ}C$ reaction temperature. The k value of catalysts shows the order of $Ce(20)/Al_2O_3=Ce(0)/Al_2O_3<Ce(5)/Al_2O_3<Ce(10)/Al_2O_3$. XRD patterns of $Ce(0)/Al_2O_3$ were no difference before and after the reaction and showed $Al_2O_3$ phases. With the increase in Ce loadings, $CeO_2$, $AlF_3$ of XRD peaks was observed. The results was indicated that Ce modifed $Al_2O_3$ than un-modifed $Al_2O_3$ was decreased reaction temperature to $200^{\circ}C$ with same decomposition rate. Also the appropriated cerium sulfate loadings on $Al_2O_3$ were 5~10 wt%.

• Proceedings of the Korean Society of Soil and Groundwater Environment Conference
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• 2005.04a
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• pp.163-166
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• 2005

[ $TiO_2$ ] 광촉매에 의한 분해 반응의 활성을 높이기 위한 다양한 연구가 진행되었다. 광촉매 반응은 1차 반응을 따랐으며 초기농도가 높을수록 분해효율이 감소하는 경향을 보였다. 본 연구에서는 산화제로 과산화수소가 주입되었을 경우 분해효율을 조사하였으며, 과산화수소를 주입하였을 경우가 그렇지 않은 경우보다 더 높은 분해효율을 보였다. 또한 과산화수소 주입량을 달리했을 때, 주입량이 증가할수록 효율이 높아지다가 일정량 이상에서는 오히려 효율이 감소하는 것으로 나타났다. 따라서 과산화수소 최적첨가량이 존재함을 알 수 있었다. 한편 $TiO_2$에 전이금속을 첨가하여 전이금속이 $TiO_2$ 촉매의 분해효율에 미치는 영향을 알아보았다. Pt(0.5%)-$TiO_2$가 가장 높은 분해효을을 보였으며, Pt첨가함량이 더 큰 Pt(2%)-$TiO_2$는 함량이 증가했음에도 불구하고 큰 차이는 아니지만 오히려 효율이 감소하였다. 따라서 촉매표면에서 전자와 정공이 생성되었을 때, Pt가 전자를 포획함으로써 전자와 정공의 재결합율을 감소시켜 OH라디칼을 생성할 수 있는 정공이 많아져 반응효율을 증가되는 것을 알 수 있었고, 금속에 따른 최적 첨가함량이 존재함을 알 수 있다. 반면에 Pd를 첨가했을 경우는 첨가 함량에 관계없이 모두 분해효율이 오히려 감소하는 경향을 나타냈으며 이는 전이금속 고유의 성질이나, 또는 대상물질에 따라 각기 다른 경향이 존재함을 나타내며 추가적인 연구가 필요하다고 사료된다.

• Journal of the Korean Society of Propulsion Engineers
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• v.9 no.4
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• pp.1-8
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• 2005

An experimental investigation of a microthruster that uses hydrogen peroxide as a monopropellant is described. The study comprises of preparation method of silver as a catalyst and performance evaluation of a mesoscale reactor. Reduction of silver in $H_2\;at\;500^{\circ}C$ resulted in the best reactivity of all the treatment method tested. A mesoscale reactor was built to find the optimum configuration for full decomposition of propellant. The catalyst bed was made of a glass wafer substrate sputtered with silver and had a length of 20 mm. We measured the conversion rate with varying feed rate of $H_2O_2$ and preheating temperature. With the feed rate of $H_2O_2$, the space time within the reactor varies as well. For the bed length of 20 mm, space time more than 480 s was required for full conversion.

• 한국신재생에너지학회:학술대회논문집
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• 2006.06a
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• pp.89-92
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• 2006

수소에너지는 화석연료 사용의 증가로 인한 환경오염 및 자원고갈의 문제점을 해결해 줄 수 있는 미래의 청정한 에너지이다. 현재 주 에너지원인 화석연료의 사용에 의하여 배출된 오염물질이 지구온난화와 같은 문제점들을 일으킨다. 이러한 문제점들을 없애줄 수 있는 대안 중 하나가 수소에너지이다. 수소에너지는 자원이 풍부하며 연소시에 오염물질이 배출되지 않는 장점이 있다. 수소에너지는 수소를 연소시켜서 얻는 에너지로써, 수소를 태우면 같은 무게의 가솔린 보다 3배나 많은 에너지를 방출한다. 수소를 생산하는 방법 중 가장 이상적인 방법은 물을 분해하는 방법이다. 그러나 이 방법은 수소를 대량으로 생산하기에는 아직 기술에 대한 확보가 되어있질 않으며, 경제성도 떨어진다는 단점이 있다. 현재 많이 쓰이는 방법 중 탄화수소류의 메탄을 수증기 개질하는 방법이 있다. 메탄 수증기 개질방법은 환경오염물질인 CO나 $CO_2$를 배출한다는 것과 높은 열원이 필요하다 본 연구에서는 C-H결합에너지가 낮아 메탄보다 분해하기 쉬운 부탄의 직접분해로 수소를 생산하고자 한다. 부탄 직접분해는 환경오염물질인 CO나 $CO_2$가 발생되지 않는 장점이 있다. 부탄 분해반응은 $500{\sim}1100^{\circ}C$의 범위에서 이루어 졌으며, 촉매는 탄소계인 카본블랙을 사용하였고, 촉매의 성능을 비교하기 위하여 열분해반응이 동시에 수행되었다.

• Korean Chemical Engineering Research
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• v.61 no.4
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• pp.487-495
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• 2023

Ammonia is either a crucial resource of fertilizer production for solving the food problem of mankind or an important energy source as both an eco-friendly hydrogen carrier and a carbon-free fuel. Therefore, nowadays ammonia synthesis and decomposition become promising. Then, a catalyst is required to effectively perform the ammonia synthesis and decomposition. In order to design high-performing as well as cheap novel catalysts for ammonia synthesis and decomposition, it is necessary to test huge amount of catalyst candidates, but it is inevitably time-consuming and expensive to search and analyze using only traditional approaches. Recently, new methods using machine learning which is one of the core technologies of the 4th industrial revolution that can quickly and accurately search high-performance catalysts has been emerging. In this paper, we investigate reaction mechanisms of ammonia synthesis and decomposition, and we described recent research and prospects of machine learning-driven methods that can efficiently find high-performing and economical catalysts for ammonia synthesis and decomposition.

• Clean Technology
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• v.22 no.4
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• pp.281-285
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• 2016

Cu wire catalyst was highly reactive toward catalytic wet peroxide oxidation of the highly refractory 1,4-dioxane. While complete removal of 1,4-dioxane could be achieved with the catalyst, the removed 1,4-dioxane could not totally mineralized into $CO_2$ and $H_2O$. In accordance with the disappearance of 1,4-dioxane, formaldehyde and oxalic acid were formed gradually with reaction time and they went through maxima. At around the time of maximum concentrations of these two intermediates acetaldehyde concentration was increased drastically and showed maximum value. With the disappearance of these three intermediates, formic acid together with ethylene glycol diformate began to increase gradually. The Cu wire catalyst was proved also to be highly stable against deactivation during the reaction.

• Clean Technology
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• v.21 no.2
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• pp.130-139
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• 2015

The NO oxidation process has been applied to improve a removal efficiency of NO included in exhaust gas. In this study, to produce a dry oxidant for the NO oxidation process, the catalytic H₂O₂ decomposition method was proposed. A variety of the heterogeneous solid-acidic Mn-based catalysts were prepared for the catalytic H₂O₂ decomposition and the effect of their physico-chemical properties on the catalytic H₂O₂ decomposition were investigated. The results of this study showed that the acidic sites of the Mn-based catalysts has an influence on the catalytic H₂O₂ decomposition. The Mn-based catalyst having the abundant acidic sites within the wide temperature range in NH₃-TPD shows the best performance for the catalytic H₂O₂ decomposition. Therefore, the NO oxidation efficiency, using the dry oxidant produced by the H₂O₂ decomposition over the Mn-based catalyst having the abundant acidic properties under the wide temperature range, was higher than the others. As a remarkable result, the best performances in the catalytic H₂O₂ decomposition and NO oxidation was shown when the Mn-based Fe₂O₃ support catalyst containing K component was used for the catalytic H₂O₂ decomposition.