[그림 2-1-1] 1㎾급 NG 리포밍 시스템 전면 패널=21,41,1

[그림 2-1-2] 1㎾급 NG 리포밍 시스템 후면부,죄측은 반응부,우측은 증발부=21,41,1

[그림 2-1-3] 2㎾급 가정용 연료전지 시스템(Viessman Werke)=22,42,1

[그림 2-1-4] Viessmann Werke의 개질기용 버너=23,43,1

[그림 2-1-5] European fuell cell의 가정용 연료전지 공정 구성도=23,43,1

[그림 2-1-6] 1.5㎾급 가정용 연료전지 시스템=24,44,1

[그림 3-1-1] 취기제로 사용되는 주요 유황화합물의 분자 구조=27,47,1

[그림 3-1-2] Schematic activated carbon model=28,48,1

[그림 3-1-3] TDA research사의 Geode=28,48,1

[그림 3-1-4] TDA사의 상온 탈황 흡착제의 성능 평가 실험 결과=28,48,1

[그림 3-1-5] Temperature programmed desorption=29,49,1

[그림 3-1-6] Zeolite X=30,50,1

[그림 3-1-7] Desulfurizer of Tokyo gas=31,51,1

[그림 3-1-8] Na+(이미지참조)가 표면에 흡착된 caly mineral(montmorillonite)=31,51,1

[그림 3-1-9] THT adsorption breakthrough curces of selected adsorbent=33,53,1

[그림 3-1-10] Simulation용 연료개질공정 흐름도=50,70,1

[그림 3-3-1] 원통형 리포머의 열／시스템 통합화 구성=53,73,1

[그림 3-3-2] 리포머 시스템 운전 장치=54,74,1

[그림 3-3-3] Prototype-1 운전 결과,2.5 ㎾급,냉각 방식 Case 1=63,83,1

[그림 3-3-4] Prototype-1 운전 결과,2.5 ㎾급,냉각 방식 Case 2=64,84,1

[그림 3-3-5] Prototype-1 운전 결과,2.5 ㎾급,냉각 방식 Case 3=65,85,1

[그림 3-3-6] Prototype-1 운전 결과,2.5 ㎾급,냉각 방식 Case 4=66,86,1

[그림 3-3-7] Prototype-1 2.5 ㎾급 운전시 냉각 방식에 따른 메탄 전환율과 효율의 영향=67,87,1

[그림 3-3-8] Prototype-1과 Prototype-2 2.5 ㎾급 운전 시 메탄 전환율 및 연소 챔버 하단 온도 변화=69,89,1

[그림 3-3-9] Prototype-2 리포머 버너 위치에 따른 메탄 전환율의 영향 및 리포머 주요 부위 온도,2.5 ㎾ 운전,R／B 2.44=71,91,1

[그림 3-3-10] Prototype-2 원통형 통합 반응기 주요 부분별 온도 2.5 ㎾ 용량,R／D＝2.44,S／C＝2.5,가변형 외곽 열교환 장치,버너 위치 5.5㎝,메탄화 반응기 포함=77,97,1

[그림 3-3-11] 원통형 통합 리포머의 시동 특성 및 정상상태 특성=82,102,1

[그림 3-4-1] Schematic diagram of PrOx reactor system=88,108,1

[그림 3-4-2] Schematic diagram of temperature programmed system=93,113,1

[그림 3-4-3] Schematic of diagram experimental apparatus. The insetillustrates details of the in-situ IR reactor=94,114,1

[그림 3-4-4] Effect of transition metal oxide loaded over r-Al₂O₃ on the CO conversion(Reaction condition:1% CO,1% O₂ and 60% H₂ in N₂ balance,flow rate＝100 cc／min,GHSV＝60,000 h-1(이미지참조)=96,116,1

[그림 3-4-5] Effect of transition metal oxide loaded over r-Al₂O₃ on the CO conversion(Reaction condition:1% CO,1% O₂ and 60% H₂ in N₂ balance,flow rate＝100 cc／min,GHSV＝60,000 h-1(이미지참조)=97,117,1

[그림 3-4-6] Effect of the amount of catalysts loaded over r-Al₂O₃ on the CO conversion,(b) O₂consumption and (c) selectivity(Reaction conditions:1% CO,1% O₂ and 60% H₂ in N₂ balance,flow rate＝100 cc／min,GHSV＝60,000 h-1(이미지참조)=100,120,1

[그림 3-4-7] Effect of weight ratio(＝Cu／(Cu+Ce))on the (a) CO conversion,(b) O₂ consumption and (c) seletivity with the reaction temperature for the selective oxidation of CO over Cu-Ce based catalysts. Reaction condirions:1% CO,1% O₂ 60% H₂,N₂ as b=101,121,1

[그림 3-4-8] Effect of various support over Cu-Ce based catalyst on the (a) CO condversion,(b) O₂ consumption,and (c) seletivity(Reaction conditions:1% CO,1% O₂ and 60% H₂ in N₂ balance,flow rate＝100 cc／min,GHSV＝60,000 h-1(이미지참조)=103,123,1

[그림 3-4-9] Effect of various transition metal addition to Cu-Ce／r-Al₂O₃ catalyst on the (a) CO conversion,(b) O₂ consumption,and (c) selectivity(Reaction conditions:1% CO,1% O₂ and 60% H₂ in N₂ balance,flow rate＝100 cc／min,GHSV＝60,000 h-1(이미=105,125,1

[그림 3-4-10] Effect of Co addition to Cu-Ce／r-Al₂O₃ catalyst on the (a) CO conversion,(b) O₂ consumption,and (c) selectivity(Reaction conditions:1% CO,1% O₂ and 60% H₂ in N₂ balance,total flow rate＝100 cc／min,GHSV＝60,000 h-1(이미지참조)=107,127,1

[그림 3-4-11] Change in the (a) CO conversion,(b) O₂consumption and (c) selectivity with λ for the reaction over Cu-Ce(4:16wt%)／r-Al₂O₃ catalyst(Reaction composition:1% CO,0.5~1.5% O₂,60% H₂,13% CO₂ 10% H₂O,N₂ as balance,feed rate:100 cc／min,G=109,129,1

[그림 3-4-12] Change in (a) CO conversion,(b) O₂consumption and (c) selectivity with λ for the reaction over Cu-Ce-Co(4.0:15.8:0.2 wt%) catalyst (Reaction composition:1% CO,0.5~1.25% O₂,60% H₂,N₂ as balance,feed rate＝100 cc／min,GHSV＝60,000 h-1(이=110,130,1

[그림 3-4-13] Change in the (a) Co conversion,(b) O₂ consumption and (c) selectivity depending on the presence of CO₂ in the reactant for the selective oxidation of CO over CuCe／A(circle) and CuCeCo0.2／A(이미지참조) (triangle down)(Solid sysmbol＝with=113,133,1

[그림 3-4-14] Change in the (a) Co conversion,(b) O₂ consumption and (c) selectivity depending on the presence of H₂O in the reactant for the selective oxidation of CO over CuCe／A(circle) and CuCeCo0.2／A(이미지참조) (triangle down)(Solid sysmbol＝with=116,136,1

[그림 3-4-15] Change in the (a) Co conversion,(b) O₂ consumption and (c) selectivity depending on the presence of H₂O and CO₂ in the reactant for the selective oxidation of CO over CuCe／A(circle) and CuCeCo0.2／A(이미지참조) (triangle down)(Solid sysm=119,139,1

[그림 3-4-16] Reverse water-gas shift(circle) and methanation(reverse triangle) activities of CuCe／A(solid). Reaction condition:1%CO₂+60% H₂in N₂balance,flow rate＝100 cc／min.=122,142,1

[그림 3-4-17] Reverse water-gas shift(circle) and methanation(reverse triangle) activities of CuCeCo0.2／A(solid). Reaction condition:1%CO₂+60% H₂in N₂balance,flow rate＝100 cc／min.=123,143,1

[그림 3-4-18] Deactiviation mode of CuCeCo0.2／A catalyst in the presence of CO₂and H₂O. Reaction condition:1% CO+1% O₂+60% H₂+(0~13)% CO₂,(0~10)% H₂O,flow rate＝100 cc／min,reaction temperature=125,145,1

[그림 3-4-19] Effect of GHSV on the CO conversion and delectivity over CuCeCo0.2／A catalyst. Reaction condition:1% CO,1% O₂,60% H₂ in N₂ balance=127,147,1

[그림 3-4-20] Change in the CO conversion,O₂ consumption and selectivity with the reaction time during the selective oxidation of CO over CuCeCo0.2／A catalyst. Reaction condition:1% CO+1% O₂+60% H₂+13% CO2+10% H₂O in N₂ balance,reaction temperature=129,149,1

[그림 3-4-21] Change in the (a) Co conversion,(b) O2 consumption and (c) selectivity with the reaction temperature for the selective oxidation of CO over Pt[1 wt%]／r-A12O3(circle),Ru[1 wt%]／r-A12O3(triangle down),and Cu-Ce[4:16wt%]／r-A12O3(square).Reac=132,152,1

[그림 3-4-22] Change in the (a) Co conversion,(b) O2 consumption and (c) selectivity depending on the presence of 10% H₂O and 13% Co2 in the reaction for the selective oxidation of CO over Pt[1 wt%]／r-A12O3(circle),Ru[1 wt%／r-A12O3(Squate).Reaction con=133,153,1

[그림 3-4-23] XRD patterns for pure metal oxide=135,155,1

[그림 3-4-24] XRD patterns for various r-A1₂O₃ supported catalysts=136,156,1

[그림 3-4-25] TEM micrograph of Cu-Ce based catalysts=137,157,1

[그림 3-4-26] CO-TPR prefiles for various r-A1₂O₃ supported catalysts=141,161,1

[그림 3-4-27] H2-TPR(이미지참조) profiles or various r-A1₂O₃ supported catalysts=142,162,1

[그림 3-4-28] TPO profiles for various r-A1₂O₃ supported catalysts=143,163,1

[그림 3-4-29] CO-TPD profiles for various r-A1₂O₃ supported catalysts=145,165,1

[그림 3-4-30] H₂O-TPD(이미지참조) profiles for various r-A1₂O₃ supported catalysts=147,167,1

[그림 3-4-31] CO2-TPD(이미지참조) profiles for various r-A1₂O₃ supported catalysts=148,168,1

[그림 3-4-32] In-situ FTIR spectra(CO-TPR) of (a) Ce／A,(b) Cu／A,(c) CuCe／A and (d) CuCeCo0.2／A after 10% CO／He flowing for 10 min and purging with He for 10 min at different temperatures:(1) RT,(2) 50℃,(3) 80℃,(4) 100℃,(5) 150℃,(6) 200℃,(7) 250=153,173,1

[그림 3-4-33] In-situ FTIR spectra(CO-TPD) of (1) Ce／A,(2) Cu／A,(3) CuCe／A and (4) CuCeCo0.2／A at the temperature of(a) RT,(b) 80℃,(c) 100℃ and (d) 200℃ The samples were pretreated in 10% CO／IIe flow at 300℃ for 30 min and then followed by coolin=154,174,1

[그림 3-4-34] In-situ FTIR spectra of (a) Ce／A,(b) Cu／A,(c) CuCe／A and (d) CuCeCo0.2／A at the temperature of (1) 100℃,(2) 150℃,(3) 200℃,(4) 250℃,(5) 300℃ in PrOx condition; 2% CO+2% O2+4% H₂O+15% N2 in H2 balance=155,175,1

[그림 3-4-35] In-situ FTIR spectra(TPO) of (a) Cu／A,(b) CuCe／A and (c) CuCeCo0.2／A while flowing 30 cc／min air at 80℃ The samples were pretreated at 300℃ in 10% CO／He flow for 30 min and then cooled to 80℃ in the same gas flow=156,176,1