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목차

[표제지]=0,1,1

제출문=0,2,2

요약문=III,4,4

목차=VII,8,1

List Of Figures=VIII,9,3

List Of Table=XI,12,1

제1장 서론=1,13,7

제2장 관련분야 기술의 국내ㆍ외 현황=8,20,1

제1절 국내의 경우=8,20,2

제2절 국외의 경우=9,21,2

제3장 실험=11,23,1

제1절 실험실적 규모의 슬래그 반응 실험=11,23,1

1. 시료 및 시약=11,23,2

2. 실험장치=13,25,2

3. 실험결과 및 고찰=15,27,5

가. 수재슬래그와 질산과의 반응=20,32,9

나. 수재슬래그와 염산과의 반응=29,41,9

4. 결론=38,50,1

제2절 Bench Scale 규모의 슬래그 반응 실험=39,51,1

1. Bench Scale 실험 장치=39,51,3

2. Bench Scale 실험 결과=42,54,9

3. 결론=51,63,1

제3절 반응여액으로부터 고순도 질산칼슘 회수=52,64,1

1. 질산칼슘의 현황=52,64,3

2. 질산칼슘의 회수 실험=55,67,6

3. 질산칼슘회수 실험장치=61,73,15

4. 결론=76,88,1

제4절 Pilot Plant 장치설비 및 실험=77,89,1

1. Pilot Plant 장치=77,89,18

2. Pilot Plant 시제품 제조 실험=95,107,4

제4장 결론=99,111,2

[참고문헌 등]=101,113,3

표목차

Table1. Chemical Analysis Of Recycled Silica Fume=5,17,1

Table2. Chemical Analysis Of Filtered Ca(NO₃)₂ Solution=5,17,1

Table3. Chemical Analysis Of Furnace Slag=11,23,1

Table4. Solubility Product Constants=56,68,1

Table5. Chemical Composition Of Calcium Nitrate Produced From Blaster Furnace Slag (In Pilot Plant)=98,110,1

Table6. Chemical Composition Of Sludge Produced From Blaster Furnace Slag (In Pilot Plant)=98,110,1

Table7. Chemical Composition Of Silica Produced From Blaster Furnace Slag (In Pilot Plant)=98,110,1

그림목차

Fig.1. The Process Flow Sheet Of Silica Fume From Slag=3,15,1

Fig.2. The Process Flowsheet Of Ca(NO₃)₂Synthesis With Lime=7,19,1

Fig.3. The X-ray Diffraction Analysis Of Water-quenched Slag=12,24,1

Fig.4. The Apparatus For Reaction Of Slag=14,26,1

Fig.5. S.E.M. Photographs Of Recovered Silica=17,29,1

Fig.6. X-ray Diffraction Analysis Of Recovered Silica=18,30,1

Fig.7. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.25℃ Nitric Acid=22,34,1

Fig.8. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.100℃ Nitric Acid=23,35,1

Fig.9. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.140℃ Nitric Acid=24,36,1

Fig.10. Variation Of Conversion With Concentration Of Nitric Acid=27,39,1

Fig.11. Variation Of Conversion With Amounts Of Nitric Acid (Conc.50%)=28,40,1

Fig.12. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.25℃ Hydrochloric Acid=31,43,1

Fig.13. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.100℃ Hydrochloric Acid=32,44,1

Fig.14. Variation Of Conversion With Particle Size Of Water-quenched Slag In Temp.140℃ Hydrochloric Acid=33,45,1

Fig.15. Variation Of Conversion With Concentration Of Hydrochloric Acid=34,46,1

Fig.16. Variation Of Conversion With Amounts Of Hydrochloric Acid=35,47,1

Fig.17. Variation Of Conversion With Concentration Of Hydrochloric Acid=37,49,1

Fig.18. Apparatus Of Bench Scale Process=40,52,1

Fig.19. Flowsheet Of Bench Scale Process=41,53,1

Fig.20. Variation Of Conversion With Particle Size Of Water-quenched Slag at Temp.120℃ Nitric Acid (In Bench Scale)=43,55,1

Fig.21. Variation Of Conversion With Concentration Of Nitric Acid (In Bench Scale)=45,57,1

Fig.22. Variation Of Conversion With Reaction Temp.25℃ (In Bench Scale)=46,58,1

Fig.23. Variation Of Conversion With Particle Size Of Water-quenched Slag At Temp.25℃ Hydrochloric Acid (In Bench Scale)=48,60,1

Fig.24. Variation Of Conversion With Various Slag=50,62,1

Fig.25. Flowsheet Of Process For Synthesis Of Calcium Nitrate With Limes=54,66,1

Fig.26. Flow Sheet Of Process For Synthesis Of Calcium Nitrate With Wastes=57,69,1

Fig.27. Apparatus For Crystallization Of Ca(NO₃)₂2ㆍ4H₂O=61,73,1

Fig.28. Relation Of Specific Gravity And Concentration Of Calcium Nitrate Solution=63,75,1

Fig.29. Variation Of Amount Of Ca(NO₃)₂Crystalline With Specific Gravity Of Ca(NO₃)₂Solution=65,77,1

Fig.30. Variation Of Amount Of Ca(NO₃)₂Crystalline With Solution Temperature=67,79,1

Fig.31. Variation Of Concentration Of Mother Liquor With Cooling Temperature And Concentration=69,81,1

Fig.32. Variation Of Amount Of Ca(NO₃)₂Crystalline With Cooling Temperature=71,83,1

Fig.33. Variation Of Solution Temperature With Cooling Time=72,84,1

Fig.34. pH Of Ca(NO₃)₂According To pH Of Mother Liquor=74,86,1

Fig.35. Recovered Calcium Nitrate Liquid And Ca(NO₃)₂ㆍ4H₂O=75,87,1

Fig.36. Flow Sheet Of Pilot Plant Process=78,90,1

Fig.37. Main Reactor=80,92,1

Fig.38. Main Reactor=80,92,1

Fig.39. Press Filter=82,94,1

Fig.40. Press Filter=82,94,1

Fig.41. Silica Washing Reactor=84,96,1

Fig.42. Silica Washing Reactor=84,96,1

Fig.43. Rotary Kiln Furnace=86,98,1

Fig.44. Rotary Kiln Furnace=86,98,1

Fig.45. Neutralizing Reactor=88,100,1

Fig.46. Neutralizing Reactor=88,100,1

Fig.47. Concentrating Reactor=90,102,1

Fig.48. Concentrating Reactor=90,102,1

Fig.49. Crystallizing Reactor=92,104,1

Fig.50. Crystallizing Reactor=92,104,1

Fig.51. Spin Dehydrator=94,106,1

Fig.52. Spin Dehydrator=94,106,1

Fig.53. Recovered Calcium Nitrate [Ca(NO₃)₂ㆍ4H₂O] From Pilot Plant Process=96,108,1

Fig.54. Recovered Silica Powder From Pilot Plant Process=96,108,1

Fig.55. Recovered Coagulator Powder From Pilot Plant Process=97,109,1

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