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목차

[표제지 등]=0,1,2

제출문=1,3,2

요약문=3,5,10

목차=13,15,16

제1장 서론=29,31,1

제1절 연구배경=29,31,1

제2절 연구목적 및 범위=30,32,3

제2장 오염매립지역 생물학적 안정화 기술개발 현장화 연구=33,35,1

제1절 서론=33,35,2

제2절 국내외 기술개발 현황=35,37,3

제3절 연구개발수행 내용 및 결과=38,40,1

1. 이론적 고찰=38,40,4

2. 매립지안정화를 위한 최적조건의 결정=42,44,12

3. 매립지 안정화시스템의 설계 및 제작=54,56,11

4. 매립지 안정화시스템의 현장적용결과=65,67,127

5. 본 기술의 적용사례(P시의 H매립지)=192,194,1

제4절 연구개발목표 달성도 및 대외기여도=193,195,2

제5절 연구개발결과의 활용계획=195,197,1

제6절 참고문헌=196,198,11

제3장 매립지 복원재생을 위한 감압증발 기술개발=207,209,1

제1절 서론=207,209,3

제2절 국내ㆍ외 기술개발 현황=210,212,1

1. 침출수의 특성=210,212,4

2. 침출수 처리 시스템 현황=214,216,5

3. 증발법을 이용한 처리기술=218,220,7

제3절 연구개발 수행내용 및 결과=225,227,1

1. 순환유동층열교환기의 특성=225,227,23

2. 감압증발농축처리 시스템 개발=248,250,57

3. Air-Stripping을 이용한 증발생산수중의 암모니아의 제거=305,307,21

4. VOCs(이미지참조) 및 불응축 암모니아의 제거 시스템 개발=326,328,10

5. 증발농축장치의 후처리공정으로써의 생물학적 처리공정 적용 가능성고찰=336,338,20

6. 향후연구과제=356,358,1

제4절 연구개발 목표 달성도=357,359,2

제5절 참고문헌=359,361,4

제4장 활성과산화수소를 이용한 침출수 고속고도 처리공정 개발에 관한 연구=363,365,1

제1절 서론=363,365,3

제2절 국내외 기술개발 현황=366,368,1

1. 침출수의 종류 및 정의=366,368,1

2. 침출수의 수질특성=366,368,2

3. 침출수 처리공정=368,370,9

4. 국내외 침출수 처리시스템=376,378,7

5. 과산화수소를 이용한 침출수 처리=382,384,8

제3절 연구개발 수행 내용 및 결과=390,392,1

1. 개선된 펜톤산화 공정의 개발=390,392,73

2. 고압산화 공정을 이용한 침출수 처리=463,465,19

3. 신 흡착산화 공정의 개발=482,484,37

4. 연구결과 요약=519,521,2

제4절 연구개발목표 달성도 및 대외기여도=521,523,2

제5절 연구개발결과의 활용계획=523,525,1

제6절 참고문헌=524,526,5

표목차

Table2.1-1. Summary of municipal solid waste landfill=34,36,1

Table2.2-1. Comparison of several technologies for landfill treatment=37,39,1

Table2.3.3-1. Preliminary test for effects of injection pressure=60,62,1

Table2.3.4-1. Summary of the landfill site=70,72,1

Table2.3.4-2. Characteristics of soils and gas composition in this site=72,74,1

Table2.3.4-3. Physical composition of wastes in this site(wet basis)=83,85,1

Table2.3.4-4. In situ respiration test procedure=129,131,1

Table2.3.4-5. Pressure level for monitoring points in this site=136,138,1

Table2.3.4-6. Comparison of TOC concentrations in sites with and without operation of stabilization system=137,139,1

Table2.3.4-7. Electrical resistivity, conductivity, P-wave velocity, density of landfill bulk materials(McCann, 1994)=144,146,1

Table3.2.1-1. Charateristics of Wastes in West Germany and Korea=212,214,1

Table3.2.1-2. Charateristics of leachate=212,214,1

Table3.2.1-3. Variation of leachate quality with the methods of landfiling=213,215,1

Table3.2.2-1. Charateristics of leachate with year=214,216,1

Table3.2.2-2. Leachate treatment process in Korea=215,217,1

Table3.2.2-3. Leachate treatment application ability with treatment methods(WSDE,1987)=216,218,1

Table3.2.2-4. Treatment application ability with treatment methods=217,219,1

Table3.2.2-5. Leachate treatment system in Germany(1994)=218,220,1

Table3.2.3-1. Results of leachate treatment process in Swiss=223,225,1

Table3.3.1-1. Comparison date of Conventional heat exchanger and fluidized bed heat exchanger=226,228,1

Table3.3.2-1. Results of analysis of sample A=262,264,1

Table3.3.2-2. Operating condition of apparatus=264,266,1

Table3.3.2-3. Operating condition of CFBHE apparatus=272,274,1

Table3.3.2-4. Results of leachate treatment=293,295,1

Table3.3.3-1. NH₄-N concentration and removal ratio with pH, Temperature and Air/Water ratio=313,315,1

Table3.3.5-1. characteristics of condensate into biological treatment=338,340,1

Table3.3.5-2. characteristics of microorganism in biological treatment=339,341,1

Table3.3.5-3. Results of biological treatment at steady state=346,348,1

Table3.3.5-4. Kinetic coefficient of biological treatment=349,351,1

Table3.3.5-5. Results of batch biofilm reactor=352,354,1

Table4.2-1. Leachate characteristics on the literature=367,369,1

Table4.2-2. COD/TOC, BOD, COD & evaluation of application following the lapsing period of landfill=377,379,1

Table4.2-3. Domestic municipal or industrial waste landfill leachate treatment system=378,380,1

Table4.2-4. Leachate characteristics=379,381,1

Table4.2-5. The present status & prospect of AOP application over respect industry=384,386,1

table4.3.1-1. Relative oxidizing strength of oxidants=420,422,1

table4.3.1-2. Compounds that can be oxidized by Fenton oxidation=422,424,1

table4.3.1-3. Chemicals that the Fenton oxidation does not oxidize=423,425,1

table4.3.1-4. CODH202(이미지참조) values of different concentration samples in hydrogen peroxide solution=427,429,1

table4.3.1-5. CODm values of different concentration samples in synthetic wastewater containing hydrogen peroxide and KHP=433,435,1

table4.3.1-6. Leachate treatement by the continuous advanced Fenton oxidation process=453,455,1

table4.3.1-7. Effects of reaction temperature & pH on the CODcr removal ([H₂O₂]＝4950mg/l, retention time＝2hr.)=476,478,1

table4.3.1-8. Effect of hydrogen peroxide dosage on the treatment efficiency(reaction pH＝2.5, temp.＝150℃, retention time＝30min.)=476,478,1

table4.3.1-9. Effect of ferrous sulfate dosage on the CODcr removal (reaction pH＝2.5, [H₂O₂]＝2500mg/l, retention time＝2hr.)=476,478,1

그림목차

Figure2.3.1-1. Kinetic disappearance curves=41,43,1

Figure2.3.2-1. Respirometer used in this study=43,45,1

Figure2.3.2-2a. Comparison of Accumulated oxygen uptake according to nutrient addition(N landfill)=45,47,1

Figure2.3.2-2b. Comparison of total oxygen uptake according to nutrient addition(N landfill)=45,47,1

Figure2.3.2-3. Oxygen uptake rate according to nutrient addition(N landfill, (a): no addition, (b): N addition, (c): P addition, (d): N and P addition)=46,48,1

Figure2.3.2-4. Comparison of accumualted oxygen uptake according to nutrients amount(G landfill)=48,50,1

Figure2.3.2-5. Comparison of accumualted oxygen uptake with and without trients addition(G landfill)=49,51,1

Figure2.3.2-6. Comparison of accumualted oxygen uptake according to moisture content(K landfill)=51,53,1

Figure2.3.2-7. Comparison of oxygen uptake rate according to moisture content(K landfill)=52,54,1

Figure2.3.3-1. Schematic diagram of landfill stabilization system=54,56,1

Figure2.3.3-2. Schematic of the injection well used in this study=55,57,1

Figure2.3.3-3. Schematic of the monitoring well used in this study=56,58,1

Figure2.3.4-1. Concept of stabilization for application of this technology=66,68,1

Figure2.3.4-2. Contour maps of pH and moisture content=73,75,1

Figure2.3.4-3. Contour and surface maps of volatile solids concentration=74,76,1

Figure2.3.4-4. Contour maps of Cr and Cu concentration=75,77,1

Figure2.3.4-5. Contour maps of Pb and Zn concentration=76,78,1

Figure2.3.4-6. Contour maps of As and Cd concentration=77,79,1

Figure2.3.4-7. Contour and surface maps of CH₄ concentration=78,80,1

Figure2.3.4-8. Contour and surface maps of CO₄ concentration=79,81,1

Figure2.3.4-9. Site used in this study=80,82,1

Figure2.3.4-10. Site map showing locations of injection and monitoring wells=81,83,1

Figure2.3.4-11. Excavation view of this site=82,84,1

Figure2.3.4-12. Landfill and ambient temperatures in British landfill over a two-year period. After Rees(1980b)=85,87,1

Figure2.3.4-13. Change in temperature for A-1, A-2, and A-3=88,90,1

Figure2.3.4-14. Change in temperature for B-1, B-2, and B-3=89,91,1

Figure2.3.4-15. Change in temperature for C-1, and C-2=90,92,1

Figure2.3.4-16. Change in temperature for AB-1, AB-2, and AB-3=93,95,1

Figure2.3.4-17. Change in temperature for BC-1, BC-2, and BC-3=94,96,1

Figure2.3.4-18. Change in temperature for CA-1, CA-2, and CA-3=95,97,1

Figure2.3.4-19. Change in temperature for Center=97,99,1

Figure2.3.4-20. Change in temperature for contaminated background wells=98,100,1

Figure2.3.4-21. Excavation view after 3-month period operation of stabilization system=99,101,1

Figure2.3.4-22. Excavation view after 12-month period operation of stabilization system=100,102,1

Figure2.3.4-23. Excavation view after 3-month period of other sites without operation of stabilization system=101,103,1

Figure2.3.4-24. Excavation view after 12-month period of other sites without operation of stabilization system=101,103,1

Figure2.3.4-25. Illustration of developments in gas and leachate composition(partly based on Farquhar and Rovers, 1973)=104,106,1

Figure2.3.4-26. Change in gas concentration and percent CO2/O2 for A-1=107,109,1

Figure2.3.4-27. Change in gas concentration and percent CO2/O2 for A-2=108,110,1

Figure2.3.4-28. Change in gas concentration and percent CO2/O2 for A-3=109,111,1

Figure2.3.4-29. Change in gas concentration and percent CO2/O2 for B-1=110,112,1

Figure2.3.4-30. Change in gas concentration and percent CO2/O2 for B-2=111,113,1

Figure2.3.4-31. Change in gas concentration and percent CO2/O2 for B-3=112,114,1

Figure2.3.4-32. Change in gas concentration and percent CO2/O2 for C-1=113,115,1

Figure2.3.4-33. Change in gas concentration and percent CO2/O2 for C-2=114,116,1

Figure2.3.4-34. Change in gas concentration and percent CO2/O2 for AB-1=116,118,1

Figure2.3.4-35. Change in gas concentration and percent CO2/O2 for AB-2=117,119,1

Figure2.3.4-36. Change in gas concentration and percent CO2/O2 for AB-3=118,120,1

Figure2.3.4-37. Change in gas concentration and percent CO2/O2 for BC-1=119,121,1

Figure2.3.4-38. Change in gas concentration and percent CO2/O2 for BC-2=120,122,1

Figure2.3.4-39. Change in gas concentration and percent CO2/O2 for BC-3=121,123,1

Figure2.3.4-40. Change in gas concentration and percent CO2/O2 for CA-1=122,124,1

Figure2.3.4-41. Change in gas concentration and percent CO2/O2 for CA-2=123,125,1

Figure2.3.4-42. Change in gas concentration and percent CO2/O2 for CA-3=124,126,1

Figure2.3.4-43. Change in gas concentration and percent CO2/O2 for Center=125,127,1

Figure2.3.4-44. Change in gas concentration for Con-1=126,128,1

Figure2.3.4-45. Change in gas concentration for Con-2=126,128,1

Figure2.3.4-46. Change in gas concentration for A-2a=127,129,1

Figure2.3.4-47. In situ respiration test result based on stabilization initiative without operation of stabilization system=130,132,1

Figure2.3.4-48. In situ respiration test result after 3-month period operation of stabilization system=131,133,1

Figure2.3.4-49. In situ respiration test result after 6-month period operation of stabilization system=132,134,1

Figure2.3.4-50. In situ respiration test result after 10-month period operation of stabilization system=133,135,1

Figure2.3.4-51. Comparison of in situ respiration test results according to operation period of stabilization system=134,136,1

Figure2.3.4-52. Location of the waste disposal site in G city=141,143,1

Figure2.3.4-53. Electrical resistivity of water, aquifer and impermeable beds=143,145,1

Figure2.3.4-54. Distortion of equipotentials and current flow-lines=145,147,1

Figure2.3.4-55. Pole-pole electrode configuration=147,149,1

Figure2.3.4-56. Survey depths and ranges of the three electrode configurations=148,150,1

Figure2.3.4-57. Electric potential decay curve=149,151,1

Figure2.3.4-58. Topographic corrections=152,154,1

Figure2.3.4-59. Model study for the pseudo-section and the inversions(조 유아1995)=155,157,1

Figure2.3.4-60. Survey lines at the waste disposal site=161,163,1

Figure2.3.4-61. Wenner horizontal profiling along L1=162,164,1

Figure2.3.4-62. Resisitivity pseudosection along line L2(field data)=163,165,1

Figure2.3.4-63. Electric potential decay with distances(a)field data (b)bad data discarded=164,166,1

Figure2.3.4-64. Mosaicked resistivity pseudosection (a)1998. 4 data(b)1997. 10 data=165,167,1

Figure2.3.4-65. Electric potential decay with distances=169,171,1

Figure2.3.4-66. Resistivity pseudosection=170,172,1

Figure2.3.4-67. Resistivity pseudosection=171,173,1

Figure2.3.4-68. Resistivity pseudosection=172,174,1

Figure2.3.4-69. Resistivity pseudosection=173,175,1

Figure2.3.4-70. Temporal variation of resistivity pseudosection(field data only)=174,176,1

Figure2.3.4-71. Temporal variation of resistivity pseudosection(interpolated values used in addition to field data)=175,177,1

Figure2.3.4-72. Underground resistivity structure(about 4 months later)=179,181,1

Figure2.3.4-73. Underground resistivity structure(about 5 months later)=180,182,1

Figure2.3.4-74. Underground resistivity structure(about 7 months later)=181,183,1

Figure2.3.4-75. Underground resistivity structure(about 11 months later)=182,184,1

Figure2.3.4-76. Temporal variation of underground resistivity structure=183,185,1

Figure2.3.4-77. Temporal variation of the resistivity with depth along line L3=184,186,1

Figure2.3.4-78. Railfall amount for the duration of stabilization(mm/month)=185,187,1

Figure2.3.4-79. Seismic signal obtained at the 20m~70m spread of the survey line=187,189,1

Figure2.3.5-1. Site map including location of in-situ landfill stabilization system=192,194,1

Figure3.1-1. Variation of charateristics of leachate with time=208,210,1

Figure3.2.1-1. Leachate generation mechanism=211,213,1

Figure3.2.3-2. Flow diagram of leachate treatment process in Bavarian(Germany)=220,222,1

Figure3.2.3-3. Flow diagram of leachate treatment process in Hindelbank(Swiss)=222,224,1

Figure3.2.3-4. Photograp of leachate treatment process used evaporation(Germany 120㎥/day)=224,226,1

Figure3.3.1-1. Schematic diagram of circulating fluidized bed heat exchanger=228,230,1

Figure3.3.1-2. Schematic diagram of test apparatus of fluidized heat exchange=232,234,1

Figure3.3.1-3. Heat exchange coefficient at fluidized flow(φ3mm glass bead)=234,236,1

Figure3.3.1-4. Comparison fouling data used Fe₂SO₄=235,237,1

Figure3.3.1-5. Schematic diagram of apparatus for visualization of glass bead behavior=237,239,1

Figure3.3.1-6. Relative velocity of glass bead with diameter of particle=240,242,1

Figure3.3.1-7. Collision pattern in tube=241,243,1

Figure3.3.1-8. Collision number with water velocity=242,244,1

Figure3.3.1-9. Schematic diagram of measure of return flow rate=244,246,1

Figure3.3.1-10. Percentage of return flow rate=246,248,1

Figure3.3.2-1. Comparison Boiling with Cavitaion=249,251,1

Figure3.3.2-2. Flash Evaporation apparatus=250,252,1

Figure3.3.2-3. Flow diagram flash evaporation system=252,254,1

Figure3.3.2-4. Flash evaporation system for the treatment of leachate=259,261,1

Figure3.3.2-5. Photograph of flash evaporation system=260,262,1

Figure3.3.2-6. Boiling point rise test on leachate sample B=263,265,1

Figure3.3.2-7. Products amount with time=265,267,1

Figure3.3.2-8. COD concentration of raw and concentrated water with time=267,269,1

Figure3.3.2-9. COD concentration of concentrated water with time=268,270,1

Figure3.3.2-10. Photograph of treatment result on sample A=269,271,1

Figure3.3.2-11. Cumulated treated products of evaporation treatment(Yo-chun)(이미지참조)=274,276,1

Figure3.3.2-12. Cumulated treated products of evaporation treatment(Yo-chun)(이미지참조)=275,277,1

Figure3.3.2-13. Variation of CODcr(이미지참조) concentration of Influent and effluent(Yo-chun)(이미지참조)=276,278,1

Figure3.3.2-14. Cumulated treated products of evaporation treatment(A-nam)=278,280,1

Figure3.3.2-15. Variation of Vacuum pressure and Tempreture with time(A-nam)=279,281,1

Figure3.3.2-16. Variation of CODcr(이미지참조) concentration of Influent and effluent(A-nam)=280,282,1

Figure3.3.2-17. Cumulated treated products of evaporation treatment(Dong-bu, 1st)=281,283,1

Figure3.3.2-18. Variation of Vaccum pressure and Tempreture with time(Dong-bu, 1st)=282,284,1

Figure3.3.2-19. Variation of CODcr(이미지참조) concentration of Influent and effluent(Dong-bu, 1st)=283,285,1

Figure3.3.2-20. Cumulated treated products of evaporation treatment(Dong-bu, 2nd)=284,286,1

Figure3.3.2-21. Variation of Vacuum pressure of Tempreture with time(Dong-bu, 2nd)=285,287,1

Figure3.3.2-22. Variation of CODcr(이미지참조) concentration of Influent and effluent(Dong-bu, 2nd)=286,288,1

Figure3.3.2-23. Cumulated treated products of evaporation treatment(Dong-bu, 3rd)=287,289,1

Figure3.3.2-24. Variation of Vacuum pressure and Tempreture with time(Dong-bu, 3rd)=288,290,1

Figure3.3.2-25. Variation of CODcr(이미지참조) concentration of Influent and effluent(Dong-bu, 3rd)=289,291,1

Figure3.3.2-26. Cumulated treated products of evaporation treatment(Dong-bu, 4th)=290,292,1

Figure3.3.2-27. Variation of Vacuum pressure and Tempreture with time(Dong-bu, 4th)=291,293,1

Figure3.3.2-28. Variation of CODcr(이미지 참조) concentration of Influent and effluent(Dong-bu, 4th)=292,294,1

Figure3.3.2-29. Schematic diagram of pilot plant in Pusan-Sangok Landfill site(concluded improvement system)=296,298,1

Figure3.3.2-30. Photograph of pilot plant in Pusan-Sangok Landfill site=297,299,1

Figure3.3.2-31. Vacuum pressure with operating time on pilot plant in Pusan Sangok Landfill site=298,300,1

Figure3.3.2-32. CODcr, Mn(이미지참조) Concentration with operating time on pilot plant=299,301,1

Figure3.3.2-33. COD removal efficiency with operating time on pilot plant=300,302,1

Figure3.3.2-34. Conductivity concentration & removal with operating time on pilot plant=301,303,1

Figure3.3.2-35. CODcr, Mn(이미지참조) Concentration with operating time on pilot plant=302,304,1

Figure3.3.3-1. Variation of NH₄-N concentration with pH and time=306,308,1

Figure3.3.3-2. Mole-fraction of NH₃and NH₄+(이미지참조)=307,309,1

Figure3.3.3-3. Variation of pH with time=309,311,1

Figure3.3.3-4. Variation of average temperature on effluent with time=310,312,1

Figure3.3.3-5. Schematic diagram of Air-Stripping Process=312,314,1

Figure3.3.3-6. NH₃-N removal efficiency with Temperature and Air/Water ratio on Effluent(pH 5)=314,316,1

Figure3.3.3-7. NH₃-N removal efficiency with Temperature and Air/Water ratio on Effluent(pH 8)=316,318,1

Figure3.3.3-8. NH₃-N removal efficiency with Temp. and Air/Water ratio on Effluent(pH 10)=317,319,1

Figure3.3.3-9. NH₃-N removal efficiency with Temp. and Air/Water ratio on Effluent(pH 12)=318,320,1

Figure3.3.3-10. NH₃-N removal efficiency with Temperature and Air/Water ratio (pH 5)=321,323,1

Figure3.3.3-11. NH₃-N removal efficiency with Temperature and Air/Water ratio (pH 8)=322,324,1

Figure3.3.3-12. NH₃-N removal efficiency with Temperature and Air/Water ratio (pH 10)=323,325,1

Figure3.3.3-13. NH₃-N removal efficiency with Temperature and Air/Water ratio (pH 12)=324,326,1

Figure3.3.4-1. Experimental set-up on biofiltration of VOC=329,331,1

Figure3.3.4-2. Photograph of biofiltration for the removal of NH₃(Sanggok landfill site)=331,333,1

Figure3.3.4-3. Influent NH₃concentration with operationg time=332,334,1

Figure3.3.4-4. Effluent NH₃concentration with operationg time=333,335,1

Figure3.3.4-5. NH₃Removal efficiency with operating time=334,336,1

Figure3.3.5-1. Variation of HRT, pH, D.O and Temp. during biological process=340,342,1

Figure3.3.5-2. Variation of BOD5(이미지참조)concentration(Dong-bu)=341,343,1

Figure3.3.5-3. Variation of CODcr concentration(Dong-bu)=342,344,1

Figure3.3.5-4. Variation of Microorganism concentration(Dong-bu)=343,345,1

Figure3.3.5-5. Variation of Nitrogen concentration(Dong-bu)=344,346,1

Figure3.3.5-6. Kinetic parameter of biological treatment(Dong-bu), (1/q vs. 1/S)=347,349,1

Figure3.3.5-7. Growth rate of microoraganism and specific substrate(μ vs. q)=348,350,1

Figure3.3.5-8. Schematic diagram of experimental apparatus=353,355,1

Figure3.3.5-9. Removal of organic matter using biofilm reactor=354,356,1

Figure4.3.1-1. The simple diagram of the original Fenton Oxidation=392,394,1

Figure4.3.1-2. Effect of the reaction pH on the COD removal([H₂O₂]＝1650mg/L, [FeSO₄]＝1750mg/L)=395,397,1

Figure4.3.1-3. Effect of the ferrous sulfate dosage on the COD removal by oxidation & coagulation (pH3.5, [H₂O₂]＝1650mg/L)=396,398,1

Figure4.3.1-4. Effect of hydrogen peroxide dosage on the COD removal by oxidation & coagulation (pH3.5)=398,400,1

Figure4.3.1-5. Removed COD by oxidation on the dosage of hydrogen peroxide(reaction pH:3.5)=400,402,1

Figure4.3.1-6. Effect of coagulation pH on the COD removal by coagulation [(H₂O₂)]＝1650mg/L, [FeSO₄]＝1750mg/L)=401,403,1

Figure4.3.1-7. The simple diagram of the advanced Fenton Oxidation=404,406,1

Figure4.3.1-8. The sequence diagram of the coaguation experiment using Fenton's reagent=408,410,1

Figure4.3.1-9. Effect of the reaction pH on the CODcr & CODMn(이미지참조) removals ([H₂O₂)]＝300mg/L, [FeSO₄]＝700mg/L=409,411,1

Figure4.3.1-10. Effect of the hydrogen peroxide & ferrous sulfate dosages on the CODcr removal(reaction pH＝3.5)=411,413,1

Figure4.3.1-11. Effect of the hydrogen peroxide & ferrous sulfate dosages on the CODMn(이미지참조) removal(reaction pH＝3.5)=412,414,1

Figure4.3.1-12. Comparison of CODcr(이미지참조) removal by coagulation & oxidation (reaction pH＝3.5, [H₂O₂]＝300mg/L, 500mg/L)=414,416,1

Figure4.3.1-13. Effect of the reaction pH on the CODcr(이미지참조) removal([FeSO₄]＝564mg/L~1584mg/L)=416,418,1

Figure4.3.1-14. Effect of the reaction pH on tyhe CODMn(이미지참조) removal ([FeSO₄]＝564mg/L~1584mg/L)=417,419,1

Figure4.3.1-15. Plot of the CODH202(이미지참조)value vs. the dosage of hydrogen peroxide in water solution(○: experimental, △: Kuo(1992), □: Talinli and Anderson(1992))=428,430,1

Figure4.3.1-16. Effect of hydrogen peroxide dosage on the CODKH(이미지참조)value in synthetic wastewater containing hydrogen peroxide and KHP(○: [H₂O₂]＝0mg/L, △: [H₂O₂]＝200mg/L, □: [H₂O₂]＝500mg/L)=431,433,1

Figure4.3.1-17. Effect of the KHP concentration on the CODH202(이미지참조) value in synthetic wastewater containing hydrogen peroxide and KHP (○: [KHP]＝0mg/l, ▽: [KHP]＝85mg/l, △: [KHP]＝213mg/l, □: [KHP]＝425mg/l_=432,434,1

Figure4.3.1-18. Plot of the hydrogen peroxide concentration vs. time (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l, [FeSO₄]＝1000mg/l)=435,437,1

Figure4.3.1-19. Plot of -ln[H₂O₂](이미지참조)value vs. time (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l, [FeSO₄]＝1000mg/l)=436,438,1

Figure4.3.1-20. Reaction rate constant on the reaction pH(temp.＝20℃, [H₂O₂]＝1500mg/l, [FeSO₄]＝1000mg/l)=438,440,1

Figure4.3.1-21. Effect of the reaction temperature on the CODcr(이미지참조) removal (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l, [FeSO₄]＝1000mg/l)=439,441,1

Figure4.3.1-22. Reaction rate constant on the reaction temperature (reaction pH＝2.7, [H₂O₂]＝1500mg/l, [FeSO₄]＝1000mg/l)=440,442,1

Figure4.3.1-23. Plot of the Arrhenius equation of the reaction rate constant (1/T vs. ln k)=442,444,1

Figure4.3.1-24. Effect of the hydrogen peroxide dosage on the CODcr(이미지참조) removal & hydrogen peroxide efficiency (reaction pH＝2.7, temp.＝20℃, [FeSO₄]＝1000mg/l)=443,445,1

Figure4.3.1-25. -ln[H₂O₂](이미지참조)vs. time on the ferrous sulfate dosage (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l)=444,446,1

Figure4.3.1-26. Reaction rate constant on the ferrous sulfate dosage (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l=446,448,1

Figure4.3.1-27. Effect of the ferrous sulfate dosage on the CODcr(이미지참조) removal & hydrogen peroxide efficiency (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1500mg/l)=447,449,1

Figure4.3.1-28. Comparison of CODcr(이미지참조) removal by oxidation & coagulation on the dosage of ferrous sulfate (reaction pH＝2.7, temp.＝20℃, [H₂O₂]＝1000mg/l)=448,450,1

Figure4.3.1-29. Comparison of CODcr(이미지참조) removal by oxidation & coagulation on the dosage of ferrous sulfate (reaction pH＝2.7, temp.＝20℃, [FeSO₄]＝1000mg/l)=449,451,1

Figure4.3.1-30. The schematic diagram of continuous treatment reactor of leachate=451,453,1

Figure4.3.2-1. Schematic diagram of wet oxidation batch reactor=466,468,1

Figure4.3.2-2. Effect of the reaction pH on the CODcr(이미지참조) removal (temp.＝150℃, [H₂O₂]＝1500mg/ℓ)=468,470,1

Figure4.3.2-3. Effect of the reaction temperature on the CODcr(이미지참조) removal (reaction pH＝2.0, [H₂O₂]＝1000mg/ℓ)=470,472,1

Figure4.3.2-4. Effect of the hydrogen peroxide dosage on the CODcr(이미지참조) removal & hydrogen peroxide efficiency (reaction pH＝2.0, temp.＝150℃)=472,474,1

Figure4.3.2-5. Effect of the reaction temperature on the BOD/CODcr(이미지참조) ratio (reaction pH＝2.0, [H₂O₂]＝1000mg/ℓ)=474,476,1

Figure4.3.2-6. Schematic diagram of the wet-oxidation continuous reactor=479,481,1

Figure4.3.2-7. Photograph of wet-oxidation reactor=480,482,1

Figure4.3.3-1. Schematic diagram of the adsorption-oxidation batch reactor=483,485,1

Figure4.3.3-2. The concentration of hydrogen peroxide vs. time on the concentration of AC (sample: biologically preteated leachate, [FeSO₄]＝300mg/L, [H₂O₂]＝1000mg/L, Temp＝20℃, reaction pH＝3.0)=485,487,1

Figure4.3.3-3. The concentration of hydrogen peroxide vs. time on the concentration of AC(-Ln(Ct/Co)(이미지참조) vs. time) [sample: biologically pretreated leachate, [FeSO₄]＝300mf/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=487,489,1

Figure4.3.3-4. Reaction rate constant on the concentration of AC(k vs. Conc. of AC)[sample: biologically pretreated leachate, [FeSO₄]＝300mg/L, [H₂O₂]＝1000mg/L, Temp. ＝20℃, reaction pH＝3.0]=488,490,1

Figure4.3.3-5. Comparison of the COD & calculated value(CODfinal+0.4706*[H])(이미지참조) vs. time (COD vs. time)[sample: biologically pretreted leachate, [AC]＝1000mg/L, [FeSO₄]＝100mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=489,491,1

Figure4.3.3-6. Adsorption percent of T-Fe on the concentration of AC (Percent of T-Fe adsorped vs. Conc. of AC) [sample: biologically pretreated leachate, [FeSO₄]＝300mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃ reaction pH＝3.0]=491,493,1

Figure4.3.3-7. Percent of Fe(II) on the concentration of AC (Percent of Fe(II) vs. Conc. of AC) [sample:biologically pretreated leachate, [FeSO₄]＝300mg/L(이미지참조), [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=492,494,1

Figure4.3.3-8. The concentration of hydrogen peroxide vs. time on the dosage of ferrous sulfate [sample:bilolgically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=493,495,1

Figure4.3.3-9. The concentration of ferrous sulfate vs. time on the dosage of hydrogen peroxide(-Ln(Ct/Co)(이미지참조)vs. time)[sample:biologically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=494,496,1

Figure4.3.3-10. Reaction rate constant on the dosage of ferrous sulfate(-Ln(Ct/Co)(이미지참조) vs. time) [sample:biologically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=496,498,1

Figure4.3.3-11. Plot of the hydrogen peroxide concentration us. time on the dosage of ferrous sulfate [sample:biologically pretreated leachate, [AC]500mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=497,499,1

Figure4.3.3-12. Reaction rate constant on the concentration of ferrous sulfate [sample:biologically pretreated leachate, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=498,500,1

Figure4.3.3-13. Remaining concentration of Fe(II) & T-Fe on the concentration of ferrous sulfate [sample:biologically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=499,501,1

Figure4.3.3-14. Percent of Fe(II) on the concentration of ferrous sulfate [sample:biologically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=500,502,1

Figure4.3.3-15. Removed COD & efficiency of hydrogen peroxide on the concentration of ferrous sulfate [sample:biologically pretreated leachate, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=501,503,1

Figure4.3.3-16. Reaction rate constant on the concentration of hydrogen peroxide [sample:biologically pretreated leachate,[AC]＝1000mg/L, [FeSO₄]＝300mg/L, Temp.＝20℃, reaction pH＝3.0]=503,505,1

Figure4.3.3-17. Reaction rate constant on the reaction pH [sample:biologically pretreated leachate, [AC]＝1000mg/L, [FeSO₄]＝300mg/L, [H₂O₂]＝1000mg/, Temp.＝20℃, reaction pH＝3.0]=504,506,1

Figure4.3.3-18. Schematic diagram of continuous adsorption-oxidation reactor=505,507,1

Figure4.3.3-19. Photograph of continuous adsorption-oxidation reactor=506,508,1

Figure4.3.3-20. Pilot continuous experiment[Temp.＝20℃, reaction pH＝3.0]=509,511,1

Figure4.3.3-21. Plot of the hydrogen peroxide concentration vs. time on the concentration of AC [sample:phenol solution, [FeSO₄]＝150mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=510,512,1

Figure4.3.3-22. Plot of the hydrogen peroxide concentration vs. time on the concentration of ferrous sulfate [sample:phenol solution, [AC]＝1000mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=512,514,1

Figure4.3.3-23. The concentration of hydrogen peroxide vs. time on the concentration of AC [sample:Acetic acid solution, [FeSO₄]＝150mg/L, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=513,515,1

Figure4.3.3-24. The concentration of hydrogen peroxide vs. time on the concentrations of ferrous sulfate & AC [sample:formic acid solution, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=516,518,1

Figure4.3.3-25. The concentration of formic as COD vs. time on the concentrations of ferrous sulfate & AC [sample:formic acid solution, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=517,519,1

Figure4.3.3-26. Reaction rate constant on the concentration of ferrous sulfate & AC [sample:formic acid solution, [H₂O₂]＝1000mg/L, Temp.＝20℃, reaction pH＝3.0]=518,520,1

영문목차

[title page etc.]=0,1,10

SUMMARY=9,11,2

CONTENTS=11,13,4

LIST OF TABLES=15,17,2

LIST OF FIGURES=17,19,12

CHAPTER1. Introduction=29,31,1

Section1. Background=29,31,1

Section2. Objective and scopes=30,32,3

CHAPTER2. Development of biological stabilization technology for contaminated landfill=33,35,1

Section1. Introduction=33,35,2

Section2. R&D in Korea and other contries=35,37,3

Section3. Contents and results=38,40,1

1. Theory=38,40,4

2. Determination of optimal conditions=42,44,12

3. Design and installation of stabilization system=54,56,11

4. Results=65,67,127

5. Application case=192,194,1

Section4. Achievement of objectives=193,195,2

Section5. Application plan of the research=195,197,1

Section6. Reference=196,198,11

CHAPTER3. R & D on the reduced pressure evaporation technology for the regeneration of landfill=207,209,1

Section1. Introduction=207,209,3

Section2. Present condition of R&D in country & abroad=210,212,1

1. Present condition of Leachate treatment system=210,212,4

2. Treatment technology using evaporation process=214,216,11

Section3. Contents and results of R&D=225,227,1

1. Characteristics of cirulation fluidized bed heat exchanger=225,227,23

2. Development of reduced pressure evaporation system=248,250,57

3. Removal of ammonia using Air-Stripping process=305,307,21

4. Development of removal system of VOCs=326,328,10

5. Investigation of adaptability of biological treatment process by post-treatment of evaporation process=336,338,20

6. Subject in future=356,358,1

Section4. Completion degree of an aim of R&D=357,359,2

Section5. Reference=359,361,4

CHAPTER4. A study on the high speedy and qualified leachate treatment process development using activated hydrogen peroxide=363,365,1

Section1. Introduction=363,365,3

Section2. Previous Study=366,368,1

1. The types and definition of leachate=366,368,1

2. The characteristic of leachate=366,368,2

3. The leachate treatment processes=368,370,9

4. The leachate treatment process systems of domestic and abroad nations=376,378,7

5. The leachate treatment using hydrogen peroxide=382,384,8

Section3. The Contents and Results=390,392,1

1. The development of advanced Fenton oxidation process=390,392,73

2. The leachate treatment using wet oxidation process=463,465,19

3. The leachate treatment using adsorption-oxidation process=482,484,37

4. Summary of research results=519,521,2

Section4. The Achievement and Results of Research Objects=521,523,2

Section5. The Application Plan of Research Results=523,525,1

Section6. Reference=524,526,5

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