Fig. 2-1 K-RDF 제조 공정도=29,59,1

Fig. 2-2 Fluidized bed zone=35,65,1

Fig. 2-3 순환유동층 보일러 개념도=39,69,1

Fig. 2-4 보일러 형태에 따른 분류=43,73,1

Fig. 2-5 소성온도에 대한 과잉공기량의 영향=53,83,1

Fig. 2-6 Ca／S 몰비에 따른 탈황율 및 흡수제 이용율의 변화=54,84,1

Fig. 2-7 층온도에 따른 탈황특성의 변화=55,85,1

Fig. 2-8 석회석 종류에 따른 SO₂저감특성=57,87,1

Fig. 2-9 탈황특성에 대한 흡수제 입경변화의 영향=59,89,1

Fig. 2-10 유동층에서 fuel NOx 생성과 관련된 반응경로=62,92,1

Fig. 2-11 유동층 연소에서 유연탄 연소시 질소산화물(NOx)의 로내 수직온도분포=64,94,1

Fig. 2-12 배가스중 O2 농도별 NOx 배출농도에 대한 층온도의 영향(연료입경＜ 6㎜)=66,96,1

Fig. 2-13 배가스중의 O₂농도에 따른 연료중 질소성분의 전환율(연료입경＜ 6㎜;coke 제외)=67,97,1

Fig. 2-14 연료중 질소성분의 함량별 NO로의 전환에 대한 휘발분의 영향(배가스중 8% O₂)=67,97,1

Fig. 2-15 NO 배출농도에 대한 과잉공기량의 영향=69,99,1

Fig. 2-16 0.25㎡ 단단 및 2단 유동층 연소로에서의 NOx 배출농도 비교=70,100,1

Fig. 2-17 산소농도(과잉공기량) 변화에 따른 일산화탄소의 배출특성=73,103,1

Fig. 2-18 다이옥신류와 퓨란류의 주요 생성기구=73,103,1

Fig. 2-19 도시폐기물의 소각시 다이옥신의 생성 메카니즘=75,105,1

Fig. 2-20 소각로에서 중금속의 거동=76,106,1

Fig. 3-1 RDF forming equipment and produced RDF=79,109,1

Fig. 4-1 Schematic diagram of fluidized bed incinerator of RDF=87,117,1

Fig. 4-2 Photo. of RDF incinerator=88,118,1

Fig. 4-3 Schematic diagram of vibration feeder=89,119,1

Fig. 4-4 Photo. of vibration feeder=90,120,1

Fig. 4-5 Photo. of vibrator=91,121,1

Fig. 4-6 Photo. of double cyclones=92,122,1

Fig. 4-7 TGA analysis results=95,125,1

Fig. 4-8 Umf(이미지참조) of Lab-scale fluidized bed incinerator=96,126,1

Fig. 4-9 Temperature profiles with height above the distributor=97,127,1

Fig. 4-10 Effects of air／fuel ratio on air pollutant concentration(U0(이미지참조)＝0.8㎧,Tem.:850℃)=99,129,1

Fig. 4-11 Effects of air／fuel ratio on air pollutant concentration(U0(이미지참조)＝1.0㎧,Tem.:850℃)=99,129,1

Fig. 4-12 Effects of air／fuel ratio on air pollutant concentration(U0(이미지참조)＝1.2㎧,Tem.:850℃)=100,130,1

Fig. 4-13 Effects of air／fuel ratio on air pollutant concentration(U0(이미지참조)＝1.4㎧,Tem.:850℃)=100,130,1

Fig. 4-14 Combution efficiency vs. total air-fuel ratio=101,131,1

Fig. 4-15 The concentration of gaseous pollutant with operating temperature(λT(이미지참조)＝1.2,Ca／S＝1.3,RDF)=107,137,1

Fig. 4-16 The concentration of gaseous pollutant with operating temperature(λT(이미지참조)＝1.2,Ca／S＝5.5,RDF)=107,137,1

Fig. 4-17 The concentration of gaseous pollutant with operating temperature(λT(이미지참조)＝1.2,Ca／S＝6.5,RDF)=108,138,1

Fig. 4-18 The mole fraction of gaseous pollutants with Ca／S ratio(T＝800℃,RDF)=108,138,1

Fig. 4-19 The concentration of calcium compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=109,139,1

Fig. 4-20 The concentration of phosphate compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=109,139,1

Fig. 4-21 The concentration of Aluminuim compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=110,140,1

Fig. 4-22 The concentration of sodium compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=110,140,1

Fig. 4-23 The concentration of Magnesium compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=111,141,1

Fig. 4-24 Chrome compounds distribution in combustion gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝1.3,RDF)=113,143,1

Fig. 4-25 Chrome compounds distribution in combustion gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝5.5,RDF)=113,143,1

Fig. 4-26 Chrome compounds distribution in combustion gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝6.5,RDF)=114,144,1

Fig. 4-27 Copper and lead compounds distribution in combution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝1.3,RDF)=114,144,1

Fig. 4-28 Copper and lead compounds distribution in combution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝5.5,RDF)=115,145,1

Fig. 4-29 Copper and lead compounds distribution in combution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝6.5,RDF)=115,145,1

Fig. 4-30 Zinc compounds distribution in bombution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝1.3,RDF)=116,146,1

Fig. 4-31 Zinc compounds distribution in bombution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝5.5,RDF)=116,146,1

Fig. 4-32 Zinc compounds distribution in bombution gas with operating temperature;(λT(이미지참조)＝1.2,Ca／S＝6.5,RDF)=117,147,1

Fig. 4-33 The concentration of Chrome compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=117,147,1

Fig. 4-34 The concentration of copper and lead compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=118,148,1

Fig. 4-35 The concentration of zine compounds with Ca／S ratio(T＝800℃,λT(이미지참조)＝1.2,RDF)=118,148,1

Fig. 5-1 Flow diagram of FBC design=121,151,1

Fig. 5-2 Diagram of RDF Fluidized bed combustor=129,159,1

Fig. 5-3 Diagram of rotary feeder=130,160,1

Fig. 5-4 Diagram of chain conveyor=130,160,1

Fig. 5-5 Bench scale RDF fluidized bed combustor=131,161,1

Fig. 5-6 Combustion air injection system=131,161,1

Fig. 5-7 Cyclone=131,161,1

Fig. 5-8 Air pre-heater=132,162,1

Fig. 5-9 Ca(OH)₂injection feeder=132,162,1

Fig. 5-10 Temperature acquisition system=132,162,1

Fig. 5-11 Cooling water=132,162,1

Fig. 5-12 Variation in pressure drop with superficial gas velocity for a bed sand=133,163,1

Fig. 5-13 Increasing ratio of temperature at each density and diameter of RDF=134,164,1

Fig. 5-14 Distribution of temperature in stable state of RDF combustion=135,165,1

Fig. 5-15 Distribution of gaseous pollutant concentration(1st:500ℓ／min,2nd:150ℓ／min)=137,167,1

Fig. 5-16 Distribution of gaseous pollutant concentration(1st:500ℓ／min,2nd:300ℓ／min)=137,167,1

Fig. 5-17 Distribution of gaseous pollutant concentration(1st:550ℓ／min,2nd:150ℓ／min)=138,168,1

Fig. 5-18 Distribution of gaseous pollutant concentration(1st:550ℓ／min,2nd:300ℓ／min)=138,168,1

Fig. 5-19 Distribution of gaseous pollutant concentration(1st:500ℓ／min,2nd:150ℓ／min)=141,171,1

Fig. 5-20 Distribution of gaseous pollutant concentration(1st:500ℓ／min,2nd:300ℓ／min)=141,171,1

Fig. 5-21 Distribution of gaseous pollutant concentration(1st:550ℓ／min,2nd:150ℓ／min)=142,172,1

Fig. 5-22 Distribution of gaseous pollutant concentration(1st:550ℓ／min,2nd:300ℓ／min)=142,172,1

Fig. 5-23 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 0)=144,174,1

Fig. 5-24 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 1)=144,174,1

Fig. 5-25 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 1.5)=145,175,1

Fig. 5-26 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 2)=145,175,1

Fig. 5-27 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 3)=146,176,1

Fig. 5-28 Distribution of gaseous pollutant concentration(Ca／0.5CI ＝ 5)=146,176,1

Fig. 5-29 CI concentration in exhaust gas and fly ash=147,177,1

Fig. 5-30 Temperature distribution with feeding rate in stable state=151,181,1

Fig. 5-31 Concentration of exhaust gases with second air variation(RDF feeding rate:3㎏／hr)=152,182,1

Fig. 5-32 Concentration of exhaust gases with second air variation(RDF feeding rate:4㎏／hr)=153,183,1

Fig. 5-33 Concentration of exhaust gases with second air variation(RDF feeding rate:5㎏／hr)=154,184,1

Fig. 5-34 CI concentration in exhaust gas and fly ash=156,186,1

Fig. 6-1 The experimental column for cold bed test=160,190,1

Fig. 6-2 Determination of minimum fluidizing velocity by pressure drop=162,192,1

Fig. 6-3 Axial distribution of wood,PE,MC and PA particles in a fluidized bed with the various gas velocity=163,193,1

Fig. 6-4 Effect of gas velocity on the overall mixing index of large cylindrical particles=164,194,1

Fig. 6-5 Effect of large particle's length on mixing index at U＝3*Umf(Umf ＝ 0.32㎧)=165,195,1

Fig. 6-6 Field of fluid using distributer not improved=167,197,1

Fig. 6-7 Field of fluid using distributer improved=167,197,1

Fig. 6-8 Schematic diagram of Internal CFBC=175,205,1

Fig. 6-9 Distributor of fluidized bed=178,208,1

Fig. 6-10 Schematic diagram of RDF feeder=179,209,1

Fig. 6-11 Temperature profiles along the height from air distributor=183,213,1

Fig. 6-12 Distribution of CO,NOx,SO₂concentration=183,213,1

Fig. 6-13 Distribution of temperature with time in reactor=184,214,1

Fig. 6-14 Distribution of temperature at each facility=184,214,1

Fig. 6-15 Bed zone of ICFC=189,219,1

Fig. 6-16 Distributor of ICFC=190,220,1

Fig. 6-17 Schematic diagram of ICFC=191,221,1

Fig. 7-1 Schematic diagram of CFBc pilot plant for RDF combustion=209,239,1

Fig. 7-2 Gas sampler=218,248,1

Fig. 7-3 Dust sampler=219,249,1

Fig. 7-4 ICP=220,250,1

Fig. 7-5 Temperature profile in the CFBc for incinerating RDF=223,253,1

Fig. 7-6 Typical temperature and pressure profiles in the riser with each operating condition=224,254,1

Fig. 7-7 Heat capacity profiles in the riser with each operating condition=227,257,1

Fig. 7-8 Photograph of the cyclone ash=233,263,1

Fig. 7-9 Photograph of the bag filter ash=233,263,1

Fig. 8-1 Backscattered electron image of silica sand before used=239,269,1

Fig. 8-2 Backscattered electron image of an agglomerate from fluidized bed combustion of RDF=240,270,1

Fig. 8-3 X-ray images of an agglomerate from RDF combustion for Si-component=240,270,1

Fig. 8-4 X-ray images of an agglomerate from RDF combustion for K- and Na-component=241,271,1

Fig. 8-5 X-ray images of an agglomerate from RDF combustion for Na-,Ca-and S-component=242,272,1

Fig. 8-6 X-ray images of an agglomerate from RDF combustion for P-component=243,273,1

Fig. 8-7 Backscattered electron image of a bed particle from fluidized bed combustion of RDF=243,273,1

Fig. 8-8 Line scanning results of a bed particle from RDF combustion for Si- and Ca-component=244,274,1

Fig. 8-9 Line scanning results of a bed particle from RDF combustion for Na-,P-and Fe-component=245,275,1

Fig. 8-10 Backscattered electron image of an agglomerate and a bed particle from fluidized bed combustion of RDF=247,277,1

Fig. 8-11 Backscattered electron image of an agglomerate and a bed particle after dye sludge combustion=248,278,1

Fig. 8-12 Backscattered electron image of an agglomerate and a bed particle after sewage sludge combustion=250,280,1

Fig. 8-13 Backscattered electron image of bed particle after RDF combustion=251,281,1

Fig. 8-14 Illustration of the processes of the bed agglomeration mechanism(Ohman et.al.,2000)=253,283,1

Fig. 8-15 Schematic diagram for particle-to-particle bonding(Mann et al.,1996)=255,285,1

Fig. 8-16 Schematic diagram for particle-to-fuel bonding(Mann et al.,1996)=256,286,1

Fig. 8-17 Schematic diagram for high temperature sintering(Mann et al.,1996)=256,286,1

Fig. 8-18 Step 1 of formation and growth mechanism of bed agglomeration=259,289,1

Fig. 8-19 Step 2 of formation and growth mechanism of bed agglomeration=259,289,1

Fig. 8-20 Step 3 of formation and growth mechanism of bed agglomeration=260,290,1

Fig. 8-21 Step 4 of formation and growth mechanism of bed agglomeration=260,290,1

Fig. 8-22 Step 5 of formation and growth mechanism of bed agglomeration=261,291,1

Fig. 8-23 Step 6 of formation and growth mechanism of bed agglomeration=261,291,1

Fig. 8-24 Agglomerates from commercial fluidized bed incinerator of RDF=262,292,1

Fig. 8-25 System of heat balance=271,301,1

Fig. 8-26 Mole fraction of silicate melts produced with temperature during fluidized bed combustion of eight fuels=276,306,1

Fig. 8-27 Mole fraction of silicate melts produced with S／(K₂O+Na₂O) molar ratio during fluidized bed combustion of five fuels=278,308,1

Fig. 8-28 Mole fraction of silicate melts produced with CI／(K₂O+Na₂O) molar ratio during fluidized bed combustion of five fuels=280,310,1

Fig. 8-29 Mole fraction of silicate melts produced with operating temperature during fluidized bed combustion of five fuels=282,312,1

Fig. 8-30 Mole fraction of silicate melts with λT(이미지참조) ratio during fluidized bed combustion of six fuels=282,312,1

Fig. 8-31 Mole fraction of silicate melts produced with operating pressure during fluidized bed combustion of six fuels=283,313,1

Fig. 8-32 Mapping of estimated mole fraction of silicate melt with various fuels(No. of fuel refers to Table 8-11)=307,337,1

Fig. 9-1 Mole fraction of silicate melts produced with temperature from kinds fuel combustion by using silica sand bed=311,341,1

Fig. 9-2 Mole fraction of silicate melts produced with temperature from kinds fuel combustion by using alumina sand bed=311,341,1

Fig. 9-3 Mole fraction of silicate melts produced with temperature from kinds fuel combustion by using limestone sand bed=313,343,1

Fig. 9-4 Mole fraction of silicate melts produced with temperature from kinds fuel combustion by using dolomite sand bed=313,343,1

Fig. 9-5 Mole fraction of silicate melts with Fe₂O₃／(K₂O+Na₂O) molar ratio during RDF combustion=316,346,1

Fig. 9-6 Mole fraction of silicate melts with Fe₂O₃／(K₂O+Na₂O) molar ratio during straw pellet combustion=316,346,1

Fig. 9-7 Mole fraction of silicate melts with Fe₂O5(이미지참조)／(K₂O+Na₂O) molar ratio during RDF combustion=318,348,1

Fig. 9-8 Mole fraction of silicate melts with Fe₂O5(이미지참조)／(K₂O+Na₂O) molar ratio during straw pellet combustion=318,348,1

Fig. 9-9 Mole fraction of silicate salt melt produced with bituminous coal／fuel mixing ratio during four fuels combustion=321,351,1

Fig. 9-10 Mole fraction of silicate salt melt produced with anthracite coal／fuel mixing ratio during four fuels combustion=321,351,1

Fig. 9-11 Schematic diagram of high temperature electric furnace=324,354,1

Fig. 9-12 XRD results of ash from RDF incineration=327,357,1

Fig. 9-13 Diagram for gravitational separated parts of melting slag=331,361,1

Fig. 9-14 Separation efficiency of heavy metals from slag with melting atmosphere:S-O,slowly cooled slag in oxidizing condition;S-R,slowly cooled slag in reducing condition=333,363,1

Fig. 9-15 Separation rate of heavy metal in ash with melting time=334,364,1