KR100192144B1 - Solid waste made land leachate treatment process - Google Patents

Solid waste made land leachate treatment process Download PDF

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KR100192144B1
KR100192144B1 KR1019960061360A KR19960061360A KR100192144B1 KR 100192144 B1 KR100192144 B1 KR 100192144B1 KR 1019960061360 A KR1019960061360 A KR 1019960061360A KR 19960061360 A KR19960061360 A KR 19960061360A KR 100192144 B1 KR100192144 B1 KR 100192144B1
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tank
leachate
aeration
waste landfill
leachate treatment
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KR1019960061360A
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Korean (ko)
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KR19980043483A (en
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박칠림
박철휘
유희찬
박미경
공민근
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장병주,이일쇄
주식회사대우
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/06—Contaminated groundwater or leachate

Abstract

본 발명은 도시폐기물 매립지에서 발생하는 침출수를 정화처리하는 폐기물 매립지 침출수 처리 공법에 관한 것으로, 침출수는 생분해성 유기물질 제거를 위한 상향류식 혐기성 반응조, 질산성 질소의 탈질을 위한 무산소조, 암모니아성 질소의 질산화를 위한 포기조, 난분해성 유기물질을 위한 응집침전조, 화학적 산화조, 응집침전조에서 순차적으로 처리되고, 성상이 다변화하는 침출수는 상향류식 혐기성 공정을 적용하여 후속 공정인 호기성 공정에 안정된 수질을 공급하고, 고농도의 암모니아성 질소는 포기조에서 질산성 질소로 질산화시켜 무산소조로 반송시킴으로서 제거하며, 난분해성 유기물질은 최적의 화학적 응집반응과 산화반응을 통하여 높은 효율로 제거되어 최종 유출수가 양질의 수질을 나타내게 된다.The present invention relates to a waste landfill leachate treatment method for purifying leachate generated from municipal waste landfill, the leachate is an upflow anaerobic reactor for the removal of biodegradable organic matter, an anoxic tank for the denitrification of nitrate nitrogen, ammonia nitrogen Sequential treatment in aeration tank for nitrification, coagulation sedimentation tank for hardly decomposable organic substances, chemical oxidation tank, and coagulation sedimentation tank, leachate with varying properties supplies stable water quality to the aerobic process which is a subsequent process by applying the upflow anaerobic process In addition, the high concentration of ammonia nitrogen is removed by nitrifying to nitrate nitrogen in the aeration tank and returning it to the anoxic tank, and the hardly decomposable organic substances are removed with high efficiency through the optimum chemical flocculation and oxidation reactions, so that the final effluent shows high quality water do.

Description

폐기물 매립지 침출수 처리 공법Waste Landfill Leachate Treatment Method

본 발명은 도시폐기물 매립지에서 발생하는 침출수를 정화처리하는 폐기물 매립지 침출수 처리 공법에 관한 것이다.The present invention relates to a waste landfill leachate treatment method for purifying leachate generated from municipal waste landfill.

종래의 침출수 처리공법은 년중 다변화하는 침출수 성상에 대한 처리능력이 저조하여 만족할 만한 수질을 얻지 못하였으며, 고농도 유기물질의 대부분을 재래식 혐기성 반응조의 능력부족으로 호기성 처리에 의존하여 긴 체류시간, 넓은 부지면적과 많은 에너지가 필요하였다. 이러한 조건에도 불구하고 유입수내 고농도의 질소는 거의 제거되지 않았으며, 난분해성 유기물질의 제거효율이 저조하여 화학약품의 의존도가 높아 약품비가 과다하게 소모되었다.Conventional leachate treatment methods have not been able to obtain satisfactory water quality due to the poor treatment ability of various leachate properties throughout the year, and most of the high concentrations of organic materials depend on aerobic treatment due to the lack of capacity of conventional anaerobic reactors. It required area and a lot of energy. In spite of these conditions, the high concentration of nitrogen in the influent was hardly removed, and the removal efficiency of hardly decomposable organic substances was low.

본 발명의 목적은 종래의 문제점을 해결하기 위하여 침출수는 생분해성 유기물질 제거를 위한 상향류식 혐기성 반응조, 질산성 질소의 탈질을 위한 무산소조, 암모니아성 질소의 질산화를 위한 포기조, 난분해성 유기물질을 위한 응집침전조, 화학적 산소조, 응집침전조에서 순차적으로 처리되고, 탈질 과정은 포기조에서 질산화된 질산성 질소를 무산소조로 반송시키는 폐기물 매립지 침출수 처리 공법을 제공하고자 하는 것이다.An object of the present invention is to solve the conventional problems, the leachate is an upflow anaerobic reactor for the removal of biodegradable organic substances, an anoxic tank for the denitrification of nitrate nitrogen, aeration tank for the nitrification of ammonia nitrogen, for difficult to decompose organic materials It is sequentially processed in the flocculation settling tank, chemical oxygen tank, flocculation settling tank, and the denitrification process is to provide a waste landfill leachate treatment method for returning the nitrified nitrate nitrogen in the aeration tank to an oxygen free tank.

본 발명의 폐기물 매립지 침출수 처리 공법에 의하면, 성상이 다변화하는 침출수는 상향류식 혐기성 공정을 적용하여 후속 공정인 호기성 공정에 안정된 수질을 공급하고, 고농도의 암모니아성 질소는 질산화 및 탈질공정을 통하여 제거하며, 난분해성 유기물질은 최적의 화학적 응집반응과 산화반응을 통하여 높은 효율로 제거되어 최종 유출수가 양질의 수질을 나타내게 된다.According to the waste landfill leachate treatment method of the present invention, leachate with varying properties supplies stable water quality to the aerobic process, which is a subsequent process by applying an upflow anaerobic process, and removes high concentration of ammonia nitrogen through nitrification and denitrification process. In addition, hardly decomposable organic substances are removed with high efficiency through optimal chemical flocculation and oxidation, resulting in high quality water.

도1은 본 발명의 전체 침출수 처리공정을 도시하는 개략도 이다.1 is a schematic diagram showing the entire leachate treatment process of the present invention.

도면의 주요 부호에 대한 설명Description of the main symbols in the drawings

1: 조정조 2: 상향류식 혐기성 반응조1: adjustment tank 2: upflow anaerobic reactor

3: 무산소조 4: 포기조3: anaerobic tank 4: aeration tank

5: 슬러지 반송라인 6: 호기성 유출수 반송라인5: sludge return line 6: aerobic effluent return line

7: 급속교반조 8: pH 조정조7: Rapid stirring bath 8: pH adjusting tank

9: 완속교반조 10: 약품침전조9: slow stirring 10: chemical precipitation

11:펜톤산화조 12: 급속교반조11: Fenton oxidation tank 12: Rapid stirring

13: 완속교반조 14: 약품침전조13: Slow stirring 14: Chemical precipitation

15: 방류관 16: 침전조15: discharge pipe 16: settling tank

본 발명의 침출수 처리 공정을 첨부된 도면을 참조하여 상세히 설명한다.The leachate treatment process of the present invention will be described in detail with reference to the accompanying drawings.

도1은 본 발명의 침출수 처리 공정의 개략도이다.1 is a schematic diagram of a leachate treatment process of the present invention.

국내에서 발생하는 침출수는 높은 알칼리도와 영양물질중 인(P)이 부족한 특성을 지니고 있다. 이에 따라 조정조(1)에서 (1+1)HCl 을 이용하여 pH 를 중성(pH 7)으로 조절하여 주고, KH2PO4을 이용하여 부족한 인(P)을 보충하여 상향류식 혐기성 반응조(UASB)(2)로 유입시켜 혐기성 반응조내의 혐기성 미생물에 악영향이 미치지 않도록 한다.Leachate produced in Korea is characterized by high alkalinity and lack of phosphorus (P) among nutrients. Accordingly, the pH is adjusted to neutral (pH 7) using (1 + 1) HCl in the adjusting tank (1), and the upflow anaerobic reactor (UASB) is supplemented by using KH 2 PO 4 to compensate for the insufficient phosphorus (P). It should be introduced into (2) to prevent adverse effects on the anaerobic microorganisms in the anaerobic reactor.

혐기성 반응조(2)를 여러 운전조건으로 실험한 결과 체류시간 1 일, 유기물 부하 6 kg CODcr/m3/d 정도에서 BOD 제거효율이 95 내지 98% 정도였다.The anaerobic reactor 2 was tested under various operating conditions, and the BOD removal efficiency was about 95 to 98% at a residence time of 1 day and an organic load of about 6 kg CODcr / m 3 / d.

혐기성 반응조 유출수는 무산소조(3)로 유입되며, 무산소조의 미생물 농도를 유지시키기 위해 포기조(4) 후단 침전조(16)의 슬러지를 반송라인(5)을 통하여 유입시킨다. 무산소조(3)내의 DO 농도를 0.5 mg/L 이하로 유지하도록 하며, 체류시간 1내지 2일, MLSS 1,500mg/L 의 조건으로 운전하여 포기조(4)에서 질산화된 유출수를 반송 라인(6)을 통해 반송시켜 무산소조(3)에서 탈질 반응이 일어나도록 한다.The anaerobic reactor effluent is introduced into the anaerobic tank (3), and the sludge of the settling tank (16) after the aeration tank (4) is introduced through the conveying line (5) to maintain the microbial concentration of the anaerobic tank. The concentration of DO in the oxygen-free tank 3 is maintained at 0.5 mg / L or less, and the nitridated effluent from the aeration tank 4 is returned to the return line 6 by operating at a residence time of 1 to 2 days for MLSS 1,500 mg / L. The denitrification reaction takes place in the oxygen-free tank 3 by conveying it through.

무산소조(3)에서 탈질반응에 필요한 탄소원은 혐기성 반응조 유출수에 잔여하는 유기물질을 이용하고 부족시 메탄올을 첨가하도록 한다.In the anoxic tank (3), the carbon source required for the denitrification reaction uses organic materials remaining in the anaerobic reactor effluent and adds methanol when insufficient.

이후 포기조(4)에서는 유입하는 암모니아성 질소를 질산화시키기 위하여 충분한 체류시간(5일정도)을 주고, DO 농도를 2mg/L 이상으로 유지하기 위하여 공기를 공급하며, 질산화에 의한 pH강하를 막기 위해 중탄산나트륨을 첨가한다.After the aeration tank (4) to give a sufficient residence time (about 5 days) to nitrify the incoming ammonia nitrogen, supply air to maintain the DO concentration above 2mg / L, to prevent the pH drop by nitrification Sodium bicarbonate is added.

pH 는 6내지 8정도, MLSS는 1,500 mg/L 정도로 운전하여 본 반응조에서 질산화된 질소를 탈질시키기 위해 상기에 언급한 바와 같이 무산소조(3)로 반송시킨다. 호기성 반응조를 거친 유출수는 생물학적 반응으로 제거 불가능한 난분해성 유기물질이 다량 포함되어 있으며, 이 난분해성 유기물질을 제거하기 위해서는 화학적 처리를 해야 한다.The pH is about 6 to 8, and the MLSS is operated at about 1,500 mg / L and returned to the oxygen-free tank 3 as mentioned above to denitrate the nitrified nitrogen in the reactor. The effluent from the aerobic reactor contains a large amount of hardly decomposable organic substances that cannot be removed by biological reactions, and chemically treated to remove these hardly decomposable organic substances.

이를 위해서 본 발명에서는 첫단계로 응집침전 반응을 실시하였다.To this end, in the present invention, a coagulation sedimentation reaction was carried out as a first step.

응집 반응조는 급속교반조(7), pH 조정조(8), 완속교반조(9)로 구성된다.The aggregation reaction tank is composed of a rapid stirring tank 7, a pH adjusting tank 8, and a slow stirring tank 9.

실험결과 여러 응집제중 염화제1철(FeCl3)을 사용한 경우가 우수하고 경제적이라는 결론을 얻어 본 공정에 적용하였으며, 급속교반조(7)로 염화제1철(FeCl3)과 호기성 유출수를 유입시키고 pH 조정조(8)에서 황산을 이용하여 pH 를 5 정도로 유지시키면서, 급속교반조(7)와 pH 조정조(8)를 각각 회전속도 200,200rpm, 체류시간 5,30분의 조건으로 운전하였다.Experimental results many flocculant of was applied to the present process takes the conclusion is that excellent and economical when used with ferrous chloride (FeCl 3), rapid stirring tank 7, ferrous chloride (FeCl 3) and the inlet to the aerobic effluent to While maintaining the pH at about 5 using sulfuric acid in the pH adjusting tank 8, the rapid stirring tank 7 and the pH adjusting tank 8 were operated under conditions of a rotational speed of 200,200 rpm and a residence time of 5,30 minutes, respectively.

이후 완속교반조(9)로 유입되어 30rpm, 20분의 체류시간을 거쳐 약품침전조(10)에서 1시간 동안 침전시킨다.Thereafter, it is introduced into the slow stirring tank (9) and precipitated in the chemical precipitation tank (10) for 1 hour through a residence time of 30 rpm and 20 minutes.

본 반응에서 난분해성 유기물질은 약 30%내지 45%정도 제거되며 이후 화학적 산화조로 유입된다. 화학적 산화는 과산화수소수(H2O2)와 황산철염(FeSO4)을 이용한 펜톤산화조(11)를 이용하였으며 여러 조건실험을 통하여 두 물질의 최적비 1:1.25(무게비)을 얻었다.In this reaction, the hardly decomposable organic matter is removed from about 30% to 45% and then introduced into the chemical oxidation tank. For chemical oxidation, Fenton's oxidation tank (11) using hydrogen peroxide (H 2 O 2 ) and ferrous sulfate (FeSO 4 ) was used, and the optimum ratio of the two materials was obtained by various conditions.

화학적 산화조는 200 rpm, 체류시간 60분, pH2 내지 3 정도로 운전되었으며 이후 다시 응집반응을 시켰다. 이 때 화학적 산화반응과 재응집침전 반응결과 난분해성 유기물질은 45%정도의 제거율을 나타내었다.The chemical oxidation tank was operated at 200 rpm, residence time 60 minutes, pH 2 to 3 and then coagulated again. At this time, as a result of chemical oxidation and reaggregation precipitation, the hardly degradable organic material showed removal rate of about 45%.

2차 응집반응은 상기의 펜톤산화조(11)에서 낮아진 pH를 8.5 이상으로 유지시키기 위해 수산화나트륨을 이용하였으며 급속교반조(12)의 운전조건을 200rpm, 체류시간 30분으로 하였다. 완속교반조(13)에서 충분한 반응이 일어나도록 운전조건을 30 rpm, 20분의 체류시간을 유지하여 최종 약품침전지(14)에서 60 분의 체류시간을 거친 후 최종 방류관(15)으로 배출 하였다.In the secondary flocculation reaction, sodium hydroxide was used to maintain the pH lowered in the Fenton oxidation tank 11 above 8.5, and the operating conditions of the rapid stirring tank 12 were 200 rpm and a residence time of 30 minutes. The operating conditions were maintained at 30 rpm for 20 minutes to allow sufficient reaction to occur in the slow stirring tank 13, and after 60 minutes in the final chemical precipitation battery 14, the discharge was discharged to the final discharge pipe 15. .

본 발명의 폐기물 매립지 침출수 처리 공법에 따르면, 유입되는 침출원수는 전체적으로 유기물 제거효율이 CODmn로 91%, BOD로 99%정도이며, 질소제거효율이 70%의 우수한 제거양상을 보였다.According to the waste landfill leachate treatment method of the present invention, the inflow of leachate is an organic removal efficiency of 91% CODmn, 99% BOD, nitrogen removal efficiency of 70% showed an excellent removal pattern.

Claims (1)

매립지 침출수는 조정조(1), 상향류식 혐기성 반응조(2), 다수의 무산소조(3), 다수의 포기조(4)와 침전조(16)를 거쳐 급속교반조(7), pH 조정조(8), 완속교반조(9)와 약품침전조(10)를 지나 펜톤산화조(11), 급속교반조(12), 완속교반조(13)및 약품침전조(14)에서 순차적으로 처리되고, 질산성 질소의 탈질과정중 무산소조(3)에 산소의 영향이 덜 미치도록 반송라인(6)을 호기성 침전조(16) 이후에서 연결하는 폐기물 매립지 침출수 처리공법.Landfill leachate flows through a rapid aeration tank (7), a pH adjustment tank (8), a slow aeration tank (1), an upflow anaerobic reactor (2), a number of anaerobic tanks (3), a plurality of aeration tanks (4) and a settling tank (16). After the stirring tank 9 and the chemical precipitation tank 10, they are sequentially processed in the Fenton oxidation tank 11, the rapid stirring tank 12, the slow stirring tank 13, and the chemical precipitation tank 14, and denitrification of nitrate nitrogen. Waste landfill leachate treatment method of connecting the return line (6) after the aerobic sedimentation tank (16) so that oxygen is less affected by the oxygen-free tank (3) during the process.
KR1019960061360A 1996-12-03 1996-12-03 Solid waste made land leachate treatment process KR100192144B1 (en)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100340098B1 (en) * 2000-05-08 2002-06-10 김동우 An elevated disposal process for the leakage water of reclaimed land
CN102295395A (en) * 2011-08-22 2011-12-28 西安青山环保科技有限公司 Coarse-fiber alkali-method refined wastewater-processing system and wastewater-processing method
CN104671610A (en) * 2015-02-13 2015-06-03 王桂霞 Deep treatment method of chemical wastewater
CN105948401A (en) * 2016-06-24 2016-09-21 中节能（临沂）环保能源有限公司 Combined technique for treating refuse leachate membrane concentrate

Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
CN110563284A (en) * 2019-10-18 2019-12-13 安徽职业技术学院 garment sewage treatment process

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100340098B1 (en) * 2000-05-08 2002-06-10 김동우 An elevated disposal process for the leakage water of reclaimed land
CN102295395A (en) * 2011-08-22 2011-12-28 西安青山环保科技有限公司 Coarse-fiber alkali-method refined wastewater-processing system and wastewater-processing method
CN104671610A (en) * 2015-02-13 2015-06-03 王桂霞 Deep treatment method of chemical wastewater
CN105948401A (en) * 2016-06-24 2016-09-21 中节能（临沂）环保能源有限公司 Combined technique for treating refuse leachate membrane concentrate

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