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CONTENTS
목차
제1부 해체 폐기물 재활용 기술 26
제1장 연구개발과제의 개요 42
제2장 국내·외 연구개발 현황 46
제1절 국내 폐 콘크리트 재 자원화 기술현황 46
1. 폐 콘크리트의 재자원화를 위한 기술 46
2. 폐 콘크리트 재활용기술 개발 현황 57
제2절 해외 연구개발 현황 66
1. 폐 콘크리트의 재활용에 관한 해외동향 66
2. 원자력시설 해체 콘크리트 폐기물 기술개발 현황 70
3. 방사성 콘크리트 폐기물 규제해제를 위한 재활용 시나리오 82
4. 방사성 콘크리트 폐기물 재활용 및 재사용 경제성 평가 85
5. 기술개발 조사사례에 대한 평가 106
제3절 연구결과가 국내외 기술개발 현황에서 차지하는 위치 108
제3장 연구개발 수행 내용 및 결과 110
제1절 콘크리트 해체폐기물 재활용 방안 설정 및 평가 110
1. 비원자력분야 재활용 방안 평가 110
2. 원자력분야 제한적 재활용 방안 평가 114
제2 절 콘크리트 해체폐기물 가열분쇄 감용기술 개발 124
1. 콘크리트 해체폐기물 특성 평가 124
2. 콘크리트 해체폐기물 부피감용 단위공정 시험 및 평가 128
3. 콘크리트 해체폐기물 가열분쇄 공정 개발 180
4. 콘크리트 해체폐기물 열적/기계적 감용 실증장치 제작 및 기술실증 196
제3절 콘크리트 미분말 감용 및 안정화 기술개발 203
1. 콘크리트 미분말 용출 감용 기술개발 203
2. 콘크리트 미분말 재생 및 고화공정 개발 214
3. 콘크리트 미분말 슬래깅 공정개발 및 기술실증 228
제4장 목표달성도 및 관련분야에의 기여도 242
제1절 목표달성도 242
제2절 대외기여도 242
제5장 연구개발의 활용계획 244
제6장 연구개발과정에서 수집한 해외과학기술정보 246
제7장 연구시설·장비 현황 248
제8장 참고문헌 250
제2부 HEPA 필터 폐기물 처리 기술 개발 256
제1장 연구개발과제의 개요 264
제2장 국내·외 연구개발 현황 266
제1절 국내 HEPA 필터 폐기물 처리 기술 현황 266
제2절 국외 HEPA 필터 폐기물 처리 기술 현황 268
제3절 연구결과가 국내·외 기술개발현황에서 차지하는 위치 274
제3장 연구개발 수행 내용 및 결과 276
제1절 HEPA 필터 폐기물 저준위화 및 감용단위 기술개발 276
1. HEPA 필터 폐기물 특성 평가 276
2. HEPA 필터 폐기물 단위 기술별 평가 280
3. HEPA 필터 폐기물 처리 flowsheet 개발 304
제2절 HEPA 필터 폐기물 저준위화 및 감용시스템 개발 306
1. HEPA 필터 폐기물 화학적 처리 시스템 개발 306
2. HEPA 필터 폐기물 고온 용융 처리 공정 개발 326
제4장 목표달성도 및 관련분야에의 기여도 334
제1절 목표달성도 334
제2절 대외기여도 334
제5장 연구개발의 활용계획 336
제6장 연구개발과정에서 수집한 해외과학기술정보 338
제7장 연구시설·장비 현황 340
제8장 참고문헌 341
제3부 알파 함유 유기 혼성폐기물 처리 단위기술 개발 344
제1장 연구개발과제의 개요 354
제2장 국내·외 연구개발 현황 356
제1절 소각대체기술 개발 현황 356
1. 소각대체기술 개요 356
2. 소각대체기술 개발 배경 357
3. 소각 대체기술의 기술성 분석 362
제2절 알파 유기 혼성폐기물 처리기술 현황 385
제3절 연구결과가 국내외 기술개발 현황에서 차지하는 위치 386
제3장 연구개발 수행 내용 및 결과 388
제1절 알파 유기 혼성폐기물 감용처리 단위기술 특성 평가 388
1. 알파 함유 유기 혼성폐기물 특성분석 388
2. 알파혼성 유기폐액의 열분해 가스화 및 무기물 분리 특성 평가 392
3. 실험실규모 전기화학적 NOx 처리 시험장치 설계/제작 및 분석/평가 398
제2절 알파 유기 혼성폐기물 감용처리 단위공정 성능 평가 402
1. 수증기개질 공정 성능 평가 402
2. 수증기개질가스 촉매산화 공정 성능 평가 415
3. 유기혼성폐기물 열분해/수증기개질 발생 NOx 제거 성능 평가 418
4. Uranium metaphosphate의 Uranium pyrophosphate로의 전환 반응 속도론적 해석 431
제4장 목표달성도 및 관련분야에의 기여도 442
제1절 목표달성도 442
제2절 대외기여도 442
제5장 연구개발의 활용계획 444
제6장 연구개발과정에서 수집한 해외과학기술 정보 446
제7장 연구시설·장비 현황 450
제8장 참고문헌 452
서지정보양식 457
BIBLIOGRAPHIC INFORMATION SHEET 458
제1부 해체폐기물 재활용 기술 개발 32
Table 2.1. Kind of crusher and characteristics 47
Table 2.2. Effect of temperature for cement curing agent and aggregate 57
Table 2.3. The use of recycling concrete waste 58
Table 2.4. The use of recycling aggregate 58
Table 2.5. Quality standard of recycling aggregate (KS F 2573) 59
Table 2.6. A range of size of recycling coarse aggregate for concrete (KS F 2573) 59
Table 2.7. A range of size of recycling fine aggregate for concrete (KS F 2573) 59
Table 2.8. Allowance value for hazardous substance in recycling aggregate (KS F2573) 59
Table 2.9. The use of recycling concrete (KS F 2573) 60
Table 2.10. Quality standard of recycling aggregate for road 61
Table 2.11. Standard size of recycling aggregate for subbase of road 62
Table 2.12. Standard size of recycling aggregate for size adjustment applicable to base layer 62
Table 2.13. Quality specifications of recycling aggregate 62
Table 2.14. Activity due to Co-60 71
Table 2.15. Irradiation test (2.5 X 1023 n/m²) 72
Table 2.16. Test-runs 74
Table 2.17. ScaIe-Up factor 96
Table 2.18. Estimation of concrete volume 96
Table 2.19. Estimation of concrete volume and average scenario costs for facilities 104
Table 2.20. Feasibility for recycling concrete waste evaluated by NUPEC 105
Table 3.1. Input data for exposure dose rate of RESRAD-RECYCLE 111
Table 3.2. Input data for exposure dose rate of RESRAD- BUILD 111
Table 3.3. Annual exposure dose rate of worker per 1Bq/g (RESRAD-RECYCLE) 112
Table 3.4. Annual exposure dose rate of the public per 1Bq/g (RESRAD-BUILD) 112
Table 3.5. Reference nuclide concentration for clearance according to recycling scenario 113
Table 3.7. Internal exposure dose per specific activity 119
Table 3.8. External exposure dose per specific activity 120
Table 3.9. Exposure dose per specific activity and clearance level. 121
Table 3.10. Exposure dose per specific activity and clearance level. 122
Table 3.11. Exposure does rate and clearance lever of worker for recycling of dismantled concrete waste 123
Table 3.12. Amount of dismantled concrete waste generated from NPP 124
Table 3.13. Amount of dismantled concrete waste from KRR-2 124
Table 3.14. Amount of dismantled concrete waste from UCP 125
Table 3.15. Estimation of amount of concrete waste generated from dismantled nuclear facilities using a scaling factor 125
Table 3.16. Estimation of amount of dismantled concrete waste for Kori-1 NPP using scaling factor 126
Table 3.17. Chemical composition of concrete wastes 126
Table 3.18. The characteristics of crusher 128
Table 3.19. The change of physical properties for prototype test specimen according to heating time 139
Table 3.20. Experimental conditions 161
Table 3.21. Process design concept of volume reduction for dismantled concrete waste 178
Table 3.22. Design concept of unit process for a volume reduction and self-disposal of concrete waste 179
Table 3.23. Dry density of separated aggregates 187
Table 3.24. Absorption radio of separated aggregates by lab scale demonstration 193
Table 3.25. Absorption radio of separated aggregates 197
Table 3.26. Distribution of aggregates produced from bench-scale demonstration 199
Table 3.27. Specific activity of Ni-63, Fe-55 in activate concrete aggregate 199
Table 3.28. Removal efficiency of radionuclide by scrubbing cycle 213
Table 3.29. Activity of leached solution of cement waste with sodium silicate 226
Table 3.30. Volume reduction of radioactive fine powder by slagging 229
Table 3.31. Micro hardness of slagged sample 231
Table 3.32. The physical properties of slagged fine powder sample 232
Table 3.33. Composition of slagged find powder sample 232
Table 3.34. Leached fraction of slagged find powder sample (PCT Leach Test, 7 days) 233
Table 3.35. Leached velocity of slagged find powder sample (PCT Leach Test, 7days) 234
Table 3.36. Leach rate of elements in slagged sample 235
Table 3.37. Leached rate of radioactive slagged sample (PCT Leach Test, 7days) 237
Table 3.38. Comparison of immobilization processes for concrete fine powder 238
Table 3.39. Comparison of leaching rate for standard vitrified glass by PCT-7 239
Table 3.40. Dismantled concrete waste arising at KAERI 240
Table 3.41. Facility operation cost in slagging of radioactive concrete fine powder 241
제2부 국내·외 연구개발 현황 260
Table 2.1. 국내 HEPA 필터 폐기물 처리 기술 현황 267
Table 2.2. 국외 HEPA 필터 폐기물 처리 기술 현황 273
Table 3.1. Physical characteristic of HEPA filter 277
Table 3.2. Elemental composition of HEPA filter media 277
Table 3.3. Chemical analysis for Uranium contaminated HEPA filter media 278
Table 3.4. Radioactive concentration of metal in 4.0 M HNO₃waste-solution before and after precipitation and filtration 285
Table 3.5. Radioactive concentration during leaching by 5 wt% NaOH solution 287
Table 3.6. Radioactive concentration of metal in 4.0 M HNO₃ waste-solution before and after precipitation and filtration 291
Table 3.7. The concentration of heavy metals and radionuclides in HEPA filter media generated from IMEF, RWTF, PIEF, HA, and RI in KAERI 294
Table 3.8. Leach rate of elements in the thermal-treated HEPA filter media 298
Table 3.9. Compansion of leaching rate for standard vitrified glass by PCT-7 299
Table 3.10. Laboratory-size HEPA glass fiber leaching equipment specification 306
Table 3.11. Results after leaching experiment for HEPA glass fiber contaminated with uranium 309
Table 3.12. Results after leachling experiment for HEPA glass fiber contaminated with cobalt and cesium 311
Table 3.13. Demonstration-size HEPA glass fiber leaching equipment specification 313
Table 3.14. Improvement items of demonstration-size HEPA glass fiber leaching equipment 315
Table 3.15. Results of demonstration-size HEPA glass fiber leaching experiment 319
Table 3.16. Residual radioactivity of main element in waste-solution after precipitation-filtration 322
Table 3.17. Leaching experimentt results for separator 323
Table 3.18. Leachling experimentt results for sealant 324
Table 3.19. Comparison of leaching rate for standard vitrified glass by PCT-7 332
Table 3.20. Leach rate of elements in the thermal-treated radioactive HEPA filter media 332
제3부 알파 함유 유기 혼성폐기물 처리 단위기술 개발 350
Table 2.1. Classification of Hazardous Waste With Respect To Matrix 359
Table 2.2. Rankings of the amount of off-gas and secondary waste with respect to the classification of waste treatment technology 359
Table 2.3. Destruction Efficiency of Delphi DETOX process (unstirred reactor) 363
Table 2.4. Destruction Efficiency of Direct Chemical Oxidation Process 365
Table 2.5. Oxidation rates (scale factors) for compounds at high concentrations. 367
Table 2.6. Oxidation of kerosene (predominately dodecane) at 90°C. 368
Table 2.7. Oxidation of Chloro-solvents by peroxydisulfate in sealed vessels. 368
Table 2.8. Results of DCO treatment of low concentration of PCBs (45 ppm Arochlor 1242) by oxidation in basic media, and by oxidation following hydrolysis pretreatment. Analysis is by EPA method 608; Analysis by Centre Analytical,… 368
Table 2.9. Experimental and theoretical destruction of waste (base-hydrolyzed trichloroethane) in three-stage CSTR T = 90C; V = 15 liters per vessel; flow = 0.10 liter/min; process model: rate = ka [S₂O82-](이미지참조) 369
Table 2.10. Treatment rate of acid digestion 371
Table 2.11. Summary of Typical DRE Results for Synthetica Steam Reforming 376
Table 3.1. TBP-dodecane Content of uranium and phosphate of two kinds of organic mixed waste 388
Table 3.2. Results of elemental analysis of pyrolysis residue of uranium-bearing TBP/dodecane organic liqulid and its further oxidation residue 390
Table 3.3. Experimental condition for NOx removal 400
Table 3.4. Kinetic data base of the destruction and oxidation reaction of butene, butanal and butanol (k = A Tn exp(-Ea/RT)) in units of cm³, mol, s, cal)(이미지참조) 403
Table 3.5. Simulation conditions of catalytic oxidizer for steam reformer outlet gas 416
Table 3.6. Reaction model equations examined in this kinetic study 438
Table 3.7. Sum of standard devlatioon(ΣS.D) between the the oretical master data and the experimental ones 438
제1부 해체폐기물 재활용 기술 개발 35
Fig 2.1. Jaw crusher. 47
Fig 2.2. Gyratory crusher. 48
Fig 2.3. Cone crusher. 49
Fig 2.4. Roll crusher. 50
Fig 2.5. Impact crusher. 50
Fig 2.6. Ball mill. 51
Fig 2.7. Road mill 51
Fig 2.8. Heating and crushing process. 54
Fig 2.9. Moving shape of ball in rotating mill. 55
Fig 2.10. Schematic for application of microwave. 56
Fig 2.11. DECO process of KEMA. 73
Fig 2.12. Plant of KEMA test. 73
Fig 2.13. Separated gravel and contaminated fine powder. 74
Fig 2.14. Modified mechanical grinding system in NUPEC. 75
Fig 2.15. Air-heating and grinding process. 76
Fig 2.16. Transformation of aggregate by heating. 76
Fig 2.17. Floor shaver. 77
Fig 2.18. Automatic wall shaver. 78
Fig 2.19. Isotron electro-sorb process. 80
Fig 2.20. AWD-CON process. 80
Fig 2.21. ROVCO₂ surface decontamination equipment. 81
Fig 2.22. Soda blasting equipment. 82
Fig 2.23. Flow sheet of steel scrap. 83
Fig 2.24. Specification of shielding block. 86
Fig 2.25. Deep and shallow disposal facility. 89
Fig 2.26. (a) Decision tree (Part A). 97
Fig 2.26. (b) Decision tree (Part B). 97
Fig 2.27. Flow sheet of Scenario 1. 98
Fig 2.28. Flow sheet of Scenario 2. 99
Fig 2.29. Flow sheet of Scenario 3. 100
Fig 2.30. Flow sheet of Scenario 4. 100
Fig 2.31. Flow sheet of Scenario 5. 101
Fig 2.32. Flow sheet of Scenario 6. 102
Fig 2.33. Scenario costs for a medium building. 103
Fig 2.34. Average scenario costs for facilities. 103
Fig 3.1. Example of overseas limited recycling of dismantled concrete waste. 114
Fig 3.2. Disposal canister and packing drum of radioactive waste. 115
Fig 3.3. Schematic diagram of waste drums in concrete box in the VLJ-Repository 117
Fig 3.4. XRD patterns of the heavy and the light weight concrete wastes. 127
Fig 3.5. Effect of the heating temperature on the separation of aggregate from the light concrete. 130
Fig 3.6. Effect of the heating temperature on the separation of aggregate from the heavy concrete. 130
Fig 3.7. Effects of the heating temperature on the separation of aggregates and the distribution of cobalt. 131
Fig 3.8. Effects of the heating temperature on the separation of aggregates and the distribution of cobalt. 131
Fig 3.9. Effect of washing with water on the specific activity of Co-60 in the aggregates separated from the light concrete. 132
Fig 3.10. Effect of washing with water on the specific activity of Co-60 in the aggregates separated from the heavy concrete. 132
Fig 3.11. Effect of the number of ball milling on the specific activity of Co-60 in the aggregates separated from the light concrete. 133
Fig 3.12. Effect of the number of ball millling on the specific activity of Co-60 in the aggregates separated from the heavy concrete. 133
Fig 3.13. The distribution characteristics of aggregates separated from the light concrete waste after completing second milling. 134
Fig 3.14. The specific activity of aggregates separated from the light concrete waste after completing second milling. 134
Fig 3.15. The distribution characterstics of aggregates separated from the heavy concrete waste after completing second milling. 135
Fig 3.16. The specific activity of aggregates separated from the heavy concrete waste after completing second milling. 135
Fig 3.17. High temperature slagging for the fine powder produced from the light and the heavy concrete. 136
Fig 3.18. Volume reduction of the fine powder by high temperature slagging in an arc furnace. 136
Fig 3.19. Relation of stress-transformation by heating time. 140
Fig 3.20. Comparison of compressive strength by heating time. 140
Fig 3.21. Comparison elasticity by heating time. 141
Fig 3.22. Comparison of compressive strength with elasticity coefficient. 141
Fig 3.23. Relation of stress and transformation by heating time. 142
Fig 3.24. Poission's ratio by heating time. 143
Fig 3.25. Crushing model of binary system. 147
Fig 3.26. Locking Index(LI) concept and schematic. 147
Fig 3.27. Air flow pattern and dominant particle streams in a Zig-Zag Moving Bed process. 150
Fig 3.28. Schematic representation of the particles classification, in which the previous history of the particle trajectory is taken into account. 150
Fig 3.29. Dominant particle flow rates in four complementary regions. 151
Fig 3.30. Particle flow rates between the stage of a Zig-Zag moving bed for completely absorbing product exits. 153
Fig 3.31. Illustration of the connection between Uo(i) for consecutive values of i.(이미지참조) 156
Fig 3.32. Experimental apparatus. 158
Fig 3.33. The geometry of the stage in a Zig-Zag Type Moving Bed. 159
Fig 3.34. Charactenstics of gas distribution and inlet section. 160
Fig 3.35. Details of sampling port from the Moving Bed. 160
Fig 3.36. Effects of sand size in the feed material on the fraction of sand in the overhead products (RF=200 g/min, RM=Sand(80%) + Powder(20%)).(이미지참조) 162
Fig 3.37. Effects of sand size in the feed material on the fraction of sand in the bottom products (RF=200 g/min, RM=Sand(80%) + Powder(20%)).(이미지참조) 163
Fig 3.38. Effects of feed rate(RF) on the fraction of overhead products (A : Powder, B: Sand) (dp=257.5μm, UGx10²=4 m/s).(이미지참조) 164
Fig 3.39. Effects of feed rate(RF) on the fraction of bottom products (A : Powder, B: Sand) (dp=257.5 μm, UGX 10²=4 m/s).(이미지참조) 165
Fig 3.40. Effects of gas velocity(UG) on the fraction of overhead products (A : Powder, B: Sand) (RF=200g/min, RM=Sand(80%)+Powder(20%)).(이미지참조) 167
Fig 3.41. Effects of gas velocity(UG) on the fraction of bottom products (A : Powder, B: Sand) (RF=200 g/min, RM=Sand(80%)+Powder(20%)).(이미지참조) 168
Fig 3.42. Effects of mixing ratio of powder(RF) on the fraction of overhead products (A : Powder, B: Sand) (UG x 10²=4 m/s, dp=257.5 μm).(이미지참조) 169
Fig 3.43. Effects of mixing ratio of powder(RF) on the fraction of overhead products (A : Powder, B: Sand) (UG x 10²=4 m/s, dp : 257.5 μm).(이미지참조) 170
Fig 3.44. Effects of feed material on gas velocity(UG) efficiency(Etot) in the zig-zag moving bed (dp=452.5 μm, RM=Sand(80%)+Powder(20%)).(이미지참조) 171
Fig 3.45. Effects of gas velocity(UG) on the total separation efficiency(Etot) in the zig-zag moving bed (dp=452.5 μm, RM=Sand(80%)+Powder(20%)).(이미지참조) 172
Fig 3.46. Effects of feed rate(RF) of feed material on the total separation efficiency(Etot) in the zig-zag moving bed (UG x 10²=2.5 m/s, RM=Sand(80%)+Powder(20%)).(이미지참조) 173
Fig 3.47. Effects of mixing ratio(RM) in the feed material on the total separation efficiency (Etot) in the zig-zag moving bed (UG x 10²=2.5 m/s, dp=257.5 μm).(이미지참조) 174
Fig 3.48. Effects of mixing ratio(RM) in the feed material on the total separation efficiency (Etot) in the zig-zag moving bed (UG x 10²=4.0 m/s, dp=325.5 μm).(이미지참조) 175
Fig 3.49. Effects of sand size in the feed material on the grade efficiency(G(x)) of sand in the Zig-Zag moving bed (RF=200 g/min, Rm = Sand(80%) + Powder(20%)).(이미지참조)) 176
Fig 3.50. Process concept for a volume reduction and self-disposal of dismantled concrete waste. 177
Fig 3.51. Test for a volume reduction of dismantled concrete waste. 180
Fig 3.52. Change of specific activity after sieving of the activated heavy weight concrete waste. 181
Fig 3.53. Change of specific activity after crushing and heating of the activated heavy weight concrete waste. 182
Fig 3.54. Distribution of the aggregates after heating and milling of the activated heavy concrete. 182
Fig 3.55. Overall distribution of the aggregates after heating and milling of the activated heavy weight concrete. 183
Fig 3.56. Distribution of the specific activity for the aggregate size form of uranium contaminated light weight concrete waste. 184
Fig 3.57. Specific activity and distribution of aggregates after a heating and milling of the contaminated uranium concrete waste. 185
Fig 3.58. Specific activity and distribution of aggregates after a heating and milling of the contaminated mortar concrete waste. 186
Fig 3.59. Absorption ratio of aggregated after heating and crushing. 187
Fig 3.60. Temperature change of aggregate surface into the heating chamber (Heat capacity : 10,000 W/m²). 188
Fig 3.61. Minimum temperature of the concrete w.r.t time. 189
Fig 3.62. Maximum temperature of the concrete w.r.t time. 189
Fig 3.63. Integrated thermal and mechanical treatment. 190
Fig 3.64. Process equipment for milling and crushing. 191
Fig 3.65. Lab-scale demonstration of thermal and mechanical treatment. 192
Fig 3.66. Distribution of aggregate by bench-scale demonstration. 193
Fig 3.67. Specific activity of the aggregates separated form activated concrete waste. 194
Fig 3.68. Distribution of the aggregates separated from activated concrete waste. 194
Fig 3.69. Specific activity of the aggregates separated from UCP concrete waste 195
Fig 3.70. Distribution of the aggregates separated from concrete waste. 195
Fig 3.71. Bench-scale demonstration equipment for the treatment of concrete waste. 196
Fig 3.72. Sequence of the demonstration test. 198
Fig 3.73. Distribution of the aggregates separated from activated concrete waste after demonstration test. 200
Fig 3.74. Specific activity of the aggregates separated from activated concrete waste after demonstration test. 200
Fig 3.75. Distribution of the aggregates separated from UCP concrete waste after demonstratioαon test. 201
Fig 3.76. Specific activity of the aggregates separated from UCP concrete waste after demonstration test. 201
Fig 3.77. Schematic of pilot plant. 202
Fig 3.78. Distribution of concrete fine powder below 1mm. 204
Fig 3.79. Specific activity of light weight concrete fine powder(1M-HCl, 25℃). 204
Fig 3.80. Removal efficiency of radionuclide form in various leaching solution 205
Fig 3.81. Removal efficiency of raddionuclide by electrochemical leaching 205
Fig 3.82. Picture of electrochemical leachling test. 206
Fig 3.83. Removal efficiency of uranium according to the kind of leachant. 207
Fig 3.84. Removal efficiency of uranium according to the concentration of HNO₃. 207
Fig 3.85. Removal efficiency of uranium according to the scrubbing time. 208
Fig 3.86. Removal efficiency of uranium according to the size of concrete fine powder. 209
Fig 3.87. Removal efficiency of uranium according to the number of scrubbing cycle. 209
Fig 3.88. Change of the radionuclide concentration for activated concrete fine powder by electrochemical leaching. 210
Fig 3.89. Process diagram of chemical leaching for concrete fine powder. 211
Fig 3.90. Demonstration scale (15L) of chemical leaching equipment. 212
Fig 3.91. Design concept for chemical leaching system. 213
Fig 3.92. TG-DTA analysis of the light weight concrete fine powder. 215
Fig 3.93. TG-DTA analysis of the heavy weight concrete fine powder. 215
Fig 3.94. XRD pattern of the light weight concrete fine powder. 216
Fig 3.95. XRD pattern of the heavy weight concrete fine powder. 217
Fig 3.96. Compressive strength of cemented waste form using light weight concrete fine powder. 219
Fig 3.97. Compressive strength of cemented waste form using heavy weight concrete fine powder. 219
Fig 3.98. Compressive strength of cemented waste form using light concrete fine powder with sodium silicate. 221
Fig 3.99. Compressive strength of cemented waste form using heavy concrete fine powder with sodium silicate. 221
Fig 3.100. Compressive strength of cemented waste form using light concrete fine powder with MgO. 222
Fig 3.101. Compressive strength of cemented waste form using heavy concrete fine powder with MgO. 222
Fig 3.102. Leachability index of Cs-137 and Co-60 performed by ANS 16.1. 226
Fig 3.103. Leachability index of cemented waste form with sodium silicate. 227
Fig 3.104. Leachability index of cemented waste form with MgO. 227
Fig 3.105. Picture of slagged concrete waste form and measurement of compressive strength. 230
Fig 3.106. Compressive strength of slagged waste form. 230
Fig 3.107. Leach rate of radionuclides from the slagged sample by slagging 236
Fig 3.108. SEM images of slagged samples 237
제2부 국내·외 연구개발 현황 261
Fig. 2.1. HEPA Filter leaching System in INEEL. 269
Fig. 2.2. A schematic diagram of the apparatus used for packed column leaching. 270
Fig. 2.3. Proposed chemical flowsheet for recovery of actinides from filters. 270
Fig. 2.4. Algorism of 4 step process in WINCO. 271
Fig. 2.5. Schematic diagram for Pilot-scale waste Filter dissolution process. 272
Fig. 3.1. Separated type HEPA filter. 276
Fig. 3.2. V-plate type HEPA filter. 276
Fig. 3.3. SEM image after capturing particles. 279
Fig. 3.4. The distribution of radionuclides in HEPA filter media. 279
Fig. 3.5. A schematic diagram of electrochemical leaching. 280
Fig. 3.6. Radioactive concentration during leaching by 4.0M HNO₃-0.1M Ce(IV) solution. 281
Fig. 3.7. Mixing of glass fibers with NaOH solution for leaching. 281
Fig. 3.8. Radioactive concentration during leaching by 5 wt% NaOH solution. 282
Fig. 3.9. Pressure filtration after 2.0 M HNO₃ solution leaching. 283
Fig. 3.10. Radioactive concentration during repetition leaching by 2.0 M HNO₃ solution. 283
Fig. 3.11. Radioactive concentration during repetition leaching by 4.0 M HNO₃ solution. 284
Fig. 3.12. Results of precipitation-filtration treatment for reuse of 4.0 M HNO₃ waste-solution contaminated with cobalt and cesium. 285
Fig. 3.13. Radioactive concentration during leaching by 4.0 M HNO₃-0.1M Ce(IV) solution. 286
Fig. 3.14. Radioactive concentration during leaching by 0.5 M H₂O₂-1.0M Na₂CO₃ solution. 288
Fig. 3.15. Radioactive concentration during leaching by 4.0M HNO₃ solution. 289
Fig. 3.16. Radioactive concentration during repetition leaching by 4.0M HNO₃ solution. 290
Fig. 3.17. Results of precipitation-filtration treatment for reuse of 4.0 M HNO₃ waste-solution contaminated with uranium. 291
Fig. 3.18. TGA analysis for HEPA filter media. 292
Fig. 3.19. TGA analysis for sealant. 292
Fig. 3.20. Thermal treated HEPA filter meida at 800℃. 293
Fig. 3.21. Thermal treated HEPA filter meida at 900℃. 293
Fig. 3.22. Diagram for thermal treatment of HEPA filter waste. 293
Fig. 3.23. Volatility test for low concentration of heavy metals. 295
Fig. 3.24. Volatility test for high (10 wt.%) concentration of heavy metals. 296
Fig. 3.25. Leachability test for heavy metals and surrogate nuclides. 297
Fig. 3.26. XRD data for (a) thermal treated HEPA filter media, HEPA filter media reacted with (b) ZnO, (c) PbO, and (d) SrO by thermal treatment. 301
Fig. 3.27. XRD data for HEPA filter media reacted with CrO₃, Co(NO₃)₂·6H₂O and CsNO₃ by thermal treatment. 302
Fig. 3.28. XRD data for the effect of temperature for HEPA filter media reacted with ZnO by thermal treatment. 303
Fig. 3.29. Development for the treatment flowsheet of low level radioactivity HEPA filter waste 305
Fig. 3.30. Development for the treatment flowsheet of high-level radioactivity HEPA filter waste 305
Fig. 3.31. Laboratory-size HEPA glass fiber leaching equipment image. 307
Fig. 3.32. Contaminated glass fiber sampled from HEPA filter waste. 307
Fig. 3.33. Leaching experiment by HEPA glass fiber leaching equipment. 308
Fig. 3.34. Filtrate and glass filter after leaching. 308
Fig. 3.35. Uranium concentration during repetition leaching by 4.0 M HNO₃ solution. 309
Fig. 3.36. Cobalt and cesium concentrations during repetition leaching by 4.0 M HNO₃ solution. 311
Fig. 3.37. Demonstration-size HEPA filter leaching equipment process diagram. 312
Fig. 3.38. Demonstratioon-size HEPA filter leaching equipment design drawing. 313
Fig. 3.39. Demonstration-size HEPA glass fiber leaching equipment image. 314
Fig. 3.40. Manufactured demonstration-size HEPA filter leaching equipment. 314
Fig. 3.41. Preparation for Cold HEPA filter leaching experiment. 315
Fig. 3.42. In the course of cold HEPA filter leaching experiment. 316
Fig. 3.43. After cold HEPA filter leaching experiment. 317
Fig. 3.44. Establishment in leaching equipment of hot HEPA filter. 318
Fig. 3.45. Leaching experiment of hot HEPA filter. 319
Fig. 3.46. After leaching experiment completion of hot HEPA filter. 320
Fig. 3.47. Filter frame after leaching experiment completion of hot HEPA filter. 320
Fig. 3.48. Results of precipitation-filtration of waste-solution. 321
Fig. 3.49. Pictures before and after precipitation of leaching waste-solution. 322
Fig. 3.50. HEPA filter separator. 323
Fig. 3.51. Leaching experiment sequence for separator. 323
Fig. 3.52. Leaching experiment results for separator. 324
Fig. 3.53. Leaching experiment sequence for sealant. 324
Fig. 3.54. Leaching experiment results for sealant. 325
Fig. 3.55. Volume reduction of HEPA filter media by thermal treatment. 326
Fig. 3.56. Separation test for HEPA filter media and aluminum separator. 327
Fig. 3.57. Compressive strength and microhardness for thermal treated sample. 328
Fig. 3.58. The detail drawing of graphite crucible 328
Fig. 3.59. The volume reduction in non-contaminated HEPA filter media by thermal treatment. 329
Fig. 3.60. The volume reduction and volatility test in radioactive HEPA filter media by thermal treatment. 330
Fig. 3.61. Volatility test for radioactivity HEPA filter media. 331
제3부 알바 함유 유기 혼성폐기물 처리 단위기술 개발 351
Fig. 2.1. Process flow diagram for the Direct Chemical Oxidation rocess 364
Fig. 2.2. Waste Steam Reforming Plant Developed by Thermochem. 374
Fig. 2.3. Thermodynamic Equilibrium Data for Selected Steam Reforming 374
Fig. 2.4. Process flow diagram of gas-phase reduction process (Eco Logic Process) 378
Fig. 2.5. Gas-Phase Reduction of Hazardous Organics Constituents 380
Fig. 3.1. Weight reduction pattern of two uranium-bearing TBP-dodecane waste and pure TBP at elevated temperatures under N₂ atmosphere. 389
Fig. 3.2. Morphology of pyrolysis residue of uranium-bearing TBP/dodecane organic liquid and its further oxidation residue. 390
Fig. 3.3. Powdered XRD patterns of pyrolysis residue (a) and combustion 391
Fig. 3.4. Overall reaction pathway of pyrolysis and gasification of uranium-bearing TBP 392
Fig. 3.5. A schematic diagram of lab-scale (0.2 kg-TBP/h) steam reforming process for the treatment of alpha-bearing mixed waste. 394
Fig. 3.6. Installed lab-scale (0.2 kg-TBP/h) steam reforming process for the treatment of alpha-bearing mixed waste. 395
Fig. 3.7. Samples of two Uranium-bearing TBP-dodecane waste solvents and pure TBP for the analysis of their pyrolysis gas at different temperatures. 395
Fig. 3.8. Analysis of pyrolysis gas composition of two uranium-bearing TBP/dodecane waste at 320℃, based on the pyrolysis-GC/MS analysis. 396
Fig. 3.9. Analysis of pyrolysis gas composition of two uranium-bearing TBP/dodecane waste at 600℃, based on the pyrolysis-GC/MS analysis. 397
Fig. 3.10. Analysis of pyrolysis gas composition of two uranium-bearing TBP/dodecane waste at 750℃, based on the pyrolysis-GC/MS analysis 397
Fig. 3.11. A schematic diagram of MEO process for NOx removal 398
Fig. 3.12. Lab-scale MEO process equipment for the removal of acid gases 399
Fig. 3.13. Parametric study of steam reformer for gaseous mixtures from the pyrolysis of waste TBP solution (TBP+dodecane+(UO₂) (NO₃)₂(TBP)₂) 411
Fig. 3.14. Gas residence time in steam reforming PFR at different steam feed rates, as a function of temperature and reactor length. 412
Fig. 3.15. Generation and decomposition of butadiene at different steam feed rates, as a function of temperature and reactor length. 413
Fig. 3.16. Decomposition of butadiene at different steam feed rates, as a function of temperature and reactor length. 414
Fig. 3.17. Mole fraction of incompletely oxidized species at the outlet of steam reforming PFR at different steam feed rates, as a function of temperature and reactor length. 415
Fig. 3.18. Temperature effect on the reactor performance at Φ = 0.2 and GHSV=20000h-1: (a)oxidation efficiency (η), (b) outlet mole fraction of feed UHCs, and (c) outlet mole fraction of newly generated UHCs(이미지참조) 417
Fig. 3.19. Influence of gas volumetric flow rate of 16,000-98,000 SCCM (GHSV of 10000-60000) on the oxidation efficiency of total UHCs (top figures) and emission concentrations of each UHC species (bottom figures) at three different... 417
Fig. 3.20. Changes in NO concentration with respect to time as a function of current density 418
Fig. 3.21. Changes in NO₂ concentration during the removal of NO with respect to time as a function of current density. 420
Fig. 3.22. Changes in NO concentration and NO removal efficiency by scrubbing liquid with and without Ag(II) accumulation before commencing the gas removal experiment, as a function of time. 421
Fig. 3.23. Effect of accumulation time of Ag(II) before commencing the gas removal experiment on NO concentration. 422
Fig. 3.24. Effect of AgNO₃ concentration on NO removal efficiency 423
Fig. 3.25. Effect of HNO₃ concentration at anodic solution for the removal of NO. 424
Fig. 3.26. Effect of HNO₃ concentration at anodic solution for the removal of NO₂. 424
Fig. 3.27. Effect of scrubbing liquid flow rate on NO removal efficiency 426
Fig. 3.28. Effect of gas flow rate on NO removal efficiency 426
Fig. 3.29. Effect of HNO₃ concentrations on NO₂ removal efficiency in gas scrubber II. 427
Fig. 3.30. Effect of sodium sulfite concentration for the removal of NO₂. 428
Fig. 3.31. Effect of sodium sulfide concentration for the removal of NO₂. 429
Fig. 3.32. Changes in NO, NO₂, and NOx concentrations with respect to time and the removal efficiencies of NOx through gas scrubber I, II 430
Fig. 3.33. TGA results of (U(PO₃)₄) with a heating rate of 1 ℃/min under inert atmosphere (N₂〉99.999%) 434
Fig. 3.34. TGA results of (U(PO₃)₄) with a heating rate of 2 ℃/min under inert atmosphere (N₂〉99.999%) 434
Fig. 3.35. TGA results of (U (PO₃)₄) with a heating rate of 3 ℃/min under inert atmosphere (N₂〉99.999%) 435
Fig. 3.36. TGA results of (U(PO₃)₄) with a heating rate of 4 ℃/min under inert atmosphere (N₂〉99.999%) 435
Fig. 3.37. Plots of In (B/T1.894661) versus 1/T for determination of activation energy, E.(이미지참조) 436
Fig. 3.38. Activation energy of the conversion of uranium metaphosphate (U(PO₃)₄) into uranium pyrophosphate (UP₂O7), as function of conversion, α(이미지참조) 437
Fig. 3.39. Master plots of theoretical g(a)/g(0.5) against a for various reaction models (solid lines, as enumerated in Table 3.6) and experimental values of p(y)/p(0.5) for different O₂ conditions (symbols) 439
Fig. 3.40. Determination of Z(=kO) values by plotting g(a) against (E/BR)p(y) for different O₂ condtitions 440
Fig. 3.41. Reaction progress of U(PO₃)₄ into UP₂O7 at given temperatures, as afunction of time(이미지참조) 440
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