KR100327151B1 - A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor - Google Patents
A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor Download PDFInfo
- Publication number
- KR100327151B1 KR100327151B1 KR1019990012626A KR19990012626A KR100327151B1 KR 100327151 B1 KR100327151 B1 KR 100327151B1 KR 1019990012626 A KR1019990012626 A KR 1019990012626A KR 19990012626 A KR19990012626 A KR 19990012626A KR 100327151 B1 KR100327151 B1 KR 100327151B1
- Authority
- KR
- South Korea
- Prior art keywords
- membrane
- aeration
- treatment
- activated sludge
- nitrogen
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 75
- 239000012528 membrane Substances 0.000 title claims abstract description 57
- 239000002351 wastewater Substances 0.000 title claims 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000005273 aeration Methods 0.000 claims abstract description 32
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 239000010865 sewage Substances 0.000 claims abstract description 21
- 239000012510 hollow fiber Substances 0.000 claims abstract description 17
- 238000005374 membrane filtration Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 238000004065 wastewater treatment Methods 0.000 claims description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 230000000717 retained effect Effects 0.000 claims 1
- 239000011550 stock solution Substances 0.000 claims 1
- 239000010802 sludge Substances 0.000 abstract description 39
- 230000001965 increasing effect Effects 0.000 abstract description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 7
- 239000005416 organic matter Substances 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 125000001477 organic nitrogen group Chemical group 0.000 description 5
- 229910052698 phosphorus Inorganic materials 0.000 description 5
- 239000011574 phosphorus Substances 0.000 description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 3
- 235000015097 nutrients Nutrition 0.000 description 3
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010840 domestic wastewater Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000011020 pilot scale process Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000012163 sequencing technique Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000003911 water pollution Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 206010011703 Cyanosis Diseases 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 244000052769 pathogen Species 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
Classifications
-
- 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
- C02F3/12—Activated sludge processes
-
- 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
- C02F3/06—Aerobic processes using submerged filters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
본 발명에 따라 중공사막을 이용한 막활성 슬러지법에 있어서 동일한 단일 반응조내에서 적절한 시간 프로그램으로 무산소단계, 폭기단계를 번갈아 수행하고 막여과를 폭기단계에서만 한정하여 실시함으로써 질소 제거효율을 획기적으로 높이고 막폐색을 효율적으로 억제할 수 있는 하수처리 방법이 제공된다. 이와같은 방법으로 기존의 막활성 슬러지법의 장점을 최대한 살리면서 별도의 시설 설치없이 추가로 높은 효율의 질소제거를 달성할 수 있는 하수처리 방법이 제공된다.In the membrane activated sludge method using a hollow fiber membrane according to the present invention, by performing an anoxic stage and an aeration stage alternately in an appropriate time program in the same single reactor, and limiting the membrane filtration only at the aeration stage, the nitrogen removal efficiency is dramatically increased and the membrane Provided is a sewage treatment method capable of effectively suppressing blockage. In this way, a sewage treatment method is provided that can further achieve high efficiency of nitrogen removal without installing a separate facility while maximizing the advantages of the existing membrane activated sludge method.
Description
본 발명은 중공사막 여과법과 활성 슬러지법을 이용하여 하수를 재이용이 가능한 수준으로 고도 처리하는 방법에 관한 것으로, 특히 유기물과 질소를 동시에 효율적으로 제거하는 하수 처리 방법에 관한 것이다.BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for advanced treatment of sewage to a reusable level using hollow fiber membrane filtration and activated sludge, and more particularly to a sewage treatment method for efficiently removing organic matter and nitrogen at the same time.
일반적으로, 막활성 슬러지법은 활성 슬러지 방법과 비교하여 볼 때, 설치소요 면적이 작고 자동운전이 용이하다는 점, 또한 침전조를 별도로 포함하지 않아 슬러지 벌킹 등의 문제를 원천적으로 해결할 수 있다는 점 등의 장점이 있어 소규모 하수처리 시설에 많이 활용되어 왔다. 특히, 막의 선택에 따라 처리 수질을 필요한 수준으로 조절할 수 있기 때문에 최근의 물 재이용에 대한 정책적 배려에 발맞추어 소규모 정수시설에도 많이 활용되고 있는 추세이다. 도 1에 전형적인 막활성 슬러지법인 크로스 플로우 막활성 슬러지 장치를 나타내었다. 또한, 상기 설명한 막활성 슬러지법에 있어서, 크로스 플로우 모듈의 막 분리 장치를 반응조 외부에 별도로 설치하는 대신 중공사막을 직접 반응조에 침적시키고, 흡입 압력을 걸어서 중공사 외부로 부터 중공사 안쪽으로 처리수를 뽑아내는 중공사막 활성 슬러지법이 개발되었다 [참조, Chiemchasri, C. and Yamamoto, K. 'Performance of membrane separation bioreactor at various temperature for domestic wastewater treatment', J. Membrane Science, 87 (1994); Shimizu, Y. et al., 'Filtration characteristic of hollow fiber microfiltration membranes used in membrane bioreactor for domestic wastewater treatment', Water Research, vol. 30 n10 (1996)]. 이 방법은 크로스 플로우 막활성 슬러지 방법에 비해 막의 폐색이 억제되고, 별도의 이송 펌프가 필요하지 않다는 장점을 가지고 있다. 그러나, 이러한 기존의 막활성 슬러지법들은 생물학적 산소요구량 (BOD) 또는 화학적 산소요구량 (COD) 등과 관련된 유기물 제거에는 매우 효율적이나 최근 하수처리장의 일반적인 문제점으로 제기되고 있는 질소 제거 등과 같은 고도 처리에는 매우 취약한 형편이다. 즉, 기존의 막활성 슬러지 방법의 경우 질소 제거율이 보통 활성 슬러지법 수준인 20 내지 30 % 수준에도 못미치는 등 여전히 개선해야 할 점이 많이 있다.In general, the membrane activated sludge method is smaller in installation area and easier to operate automatically than the activated sludge method, and it does not include a sedimentation tank to solve problems such as sludge bulking. Because of its advantages, it has been widely used in small sewage treatment facilities. In particular, the treatment water quality can be adjusted to the required level according to the selection of the membrane, which is being used in small water purification facilities in accordance with recent policy considerations for water reuse. 1 shows a cross flow membrane activated sludge apparatus which is a typical membrane activated sludge method. Further, in the membrane activated sludge method described above, instead of separately installing the membrane separation device of the cross flow module outside the reactor, the hollow fiber membrane is directly deposited in the reactor, and the suction pressure is applied to the treated water from the outside of the hollow fiber to the inside of the hollow fiber. A hollow fiber membrane activated sludge method has been developed [see, Chiemchasri, C. and Yamamoto, K. 'Performance of membrane separation bioreactor at various temperature for domestic wastewater treatment', J. Membrane Science, 87 (1994); Shimizu, Y. et al., 'Filtration characteristic of hollow fiber microfiltration membranes used in membrane bioreactor for domestic wastewater treatment', Water Research, vol. 30 n10 (1996)]. This method has the advantage that the blockage of the membrane is suppressed compared to the cross flow membrane activated sludge method, and a separate transfer pump is not required. However, these existing membrane-activated sludge methods are very effective for removing organic matters related to biological oxygen demand (BOD) or chemical oxygen demand (COD), but are very vulnerable to advanced treatment such as nitrogen removal, which is a general problem of sewage treatment plants. It's bad. That is, in the case of the conventional membrane activated sludge method, there is still much improvement, such as the nitrogen removal rate is less than the level of 20 to 30%, which is usually the level of activated sludge method.
또한, 종래의 중공사막을 이용한 하수 처리 방법은 원수의 유입과 폭기, 그리고 막 분리 공정이 동시에 진행되며, 연속적으로 운전되는 연속 폭기, 연속 흡입 운전 방식을 택하고 있으며, 이로 인해 유입수중의 암모니아성 질소 또는 유기질소가 단순히 질산화물로 산화되어 형태만 바뀔 뿐 근본적으로는 처리되지 않는다. 따라서, 종래의 중공사막을 이용한 하수 처리 방법에서는 처리수 중의 질산화물 농도가 여전히 높은 문제점이 존재한다.In addition, the conventional sewage treatment method using the hollow fiber membrane is the inflow and aeration of the raw water, and the membrane separation process is carried out at the same time, and the continuous aeration, continuous suction operation method that is operated continuously, and thus ammonia in the influent water Nitrogen or organic nitrogen is simply oxidized to nitric oxide, changing its form, but not essentially processed. Therefore, in the conventional sewage treatment method using hollow fiber membranes, there is still a problem that the concentration of nitric oxide in the treated water is still high.
일반적으로, 하수처리에 있어서 미 처리된 질소는 호소 부영양화를 야기하여 조류의 과다번성과 이로인한 수자원 오염을 초래하게 된다. 특히, 청색증 등을 유발하는 질소 산화물등에 의한 상수원 오염은 정수 처리시설의 고도화를 요구하여 정수 비용을 급격히 증가시키게 된다. 이렇듯 하수처리시 질소 및 인 제거의 중요성이 인식되면서, 우리나라에서도 1996년 1월 1일부터 처리수내 영양소에 대한 배출 규제를 실시하였으며, 앞으로 그 처리기준은 점차적으로 강화해 나갈 계획이다.In general, untreated nitrogen in sewage treatment causes lake eutrophication, resulting in overcrowding of algae and consequent water pollution. In particular, water pollution by nitrogen oxides, which cause cyanosis and the like, requires an advanced water treatment facility, thereby rapidly increasing water purification costs. As the importance of removing nitrogen and phosphorus in sewage treatment has been recognized, Korea has also regulated the emission of nutrients in treated water from January 1, 1996, and plans to gradually strengthen the treatment standards.
지금까지 기존의 활성 슬러지법을 변형하여 질소 및 인을 동시에 처리하고자 하는 많은 기술 (Biological Nutrient Removal: BNR)들이 개발되어 왔으며 현재에도 많은 기술 개선이 이루어지고 있다 (참조, 도 2). 현재 사용되고 있는 소규모 하수처리 방법들의 장단점을 요약하여 표 1에 나타내었다.Until now, a number of techniques (Biological Nutrient Removal) (BNR) have been developed to treat nitrogen and phosphorus simultaneously by modifying the existing activated sludge method and many technical improvements have been made (see FIG. 2). Table 1 summarizes the advantages and disadvantages of current small sewage treatment methods.
본 발명자들은 상기와 같은 문제점을 해결하기 위하여 상기 표 1에 열거된 기존 처리방법 중 소규모 처리 방법으로 적합한 막활성 슬러지법의 장점을 최대한 살리면서 질소제거 효율을 획기적으로 개선할 수 있는 공정을 개발하고자 예의 연구를 거듭하였다. 특히, 기존 막활성 슬러지 방법 중에서 막면적이 크고 막의 폐색이 잘 일어나지 않는 것으로 알려진 침지형 중공사막 활성 슬러지 방법을 대상으로 하여 기존의 운전방식을 개선하고자 하였다. 그 결과, 상기 중공사막을 사용한 폐수 처리 방법에서 연속 폭기, 연속 흡입 방식 대신에 간헐 폭기 및 간헐 흡입 방식을 선택하여 반응조내에 폭기 조건과 무산소 조건을 번갈아 제공함으로써 질산화와 탈질화에 의한 질소 제거가 촉진될 수 있다는 것을 발견하여 본 발명에 이르게 되었다.The inventors of the present invention intend to develop a process that can drastically improve the nitrogen removal efficiency while maximizing the advantages of the membrane activated sludge method as a small-scale treatment method among the existing treatment methods listed in Table 1 to solve the above problems. A lot of research has been conducted. In particular, we tried to improve the existing operation method for the immersion type hollow fiber membrane activated sludge method, which is known to have a large membrane area and less obstruction of membrane active sludge method. As a result, in the wastewater treatment method using the hollow fiber membrane, instead of the continuous aeration and the continuous suction method, the intermittent aeration and the intermittent suction method are selected to alternately provide aeration conditions and anoxic conditions in the reaction tank to promote nitrogen removal by nitrification and denitrification. It has been found that the present invention has led to the present invention.
즉, 본 발명에 따라 흡입식 중공사막을 이용한 폐수처리 방법에 있어서, 반응조 원액을 직접 고액 분리하여 처리수를 뽑아내는 폐수처리 방법에서, 폭기 단계 및 무산소단계를 동일한 단일 반응조내에서 교차시킴으로써 질산화 및 탈질화 반응을 유도하여 하수중 질소 처리를 촉진하는 것을 특징으로 하는 폐수처리 방법이 제공된다.That is, in the wastewater treatment method using the inhalation hollow fiber membrane according to the present invention, in the wastewater treatment method of directly extracting the treated water by solid-liquid separation of the reactor crude liquid, nitrification and denitrification by crossing the aeration stage and the anoxic stage in the same single reactor. Provided is a wastewater treatment method which induces a reaction to promote nitrogen treatment in sewage.
상기 설명한 바와 같은 본 발명의 방법에 따라, 종래의 막활성 슬러지 공정에 추가적인 시설의 설치없이 운전 방식의 개선만을 통해서 질소 제거효율을 높일 수 있다. 즉, 단일 반응조내에서 유기물 제거와 질소제거 및 고액 분리가 모두 일어나기 때문에 추가적인 반응조나 이송펌프가 필요하지 않아 소요부지 면적을 최소화할 수 있다.According to the method of the present invention as described above, it is possible to increase the nitrogen removal efficiency only through the improvement of the operation method without installing additional facilities in the conventional membrane activated sludge process. That is, since both organic matter removal, nitrogen removal, and solid-liquid separation occur in a single reactor, no additional reactor or transfer pump is required, thereby minimizing the required site area.
또한, 막을 이용하지 않는 종래의 질소 제거 하수처리 공정과 비교하여 볼 때, 본 공정은 반응조내의 미생물 농도를 훨씬 높게 유지할 수 있기 때문에 유기물이나 질소의 처리 효율을 높게 유지하면서 동시에 수리학적 체류시간을 대폭 줄일 수 있어 결과적으로 같은 면적의 반응조에 대해 단위시간당 처리 용량이 증가된다는 장점이 있다.In addition, compared with the conventional nitrogen removal sewage treatment process which does not use a membrane, this process can maintain a much higher concentration of microorganisms in the reaction tank, thereby maintaining a high treatment efficiency of organic matter or nitrogen, and at the same time, significantly reducing hydraulic retention time. As a result, the treatment capacity per unit time is increased for the reactor having the same area.
도 1은 종래의 막활성 슬러지법 (Membrane Bioreactor)을 이용한 하수처리에 사용되는 시스템의 개략도.1 is a schematic diagram of a system used for sewage treatment using a conventional membrane activated sludge method (Membrane Bioreactor).
도 2는 종래의 연속회분식 반응조 (Sequencing Batch Reactor)를 이용하는 하수의 고도처리 방법을 나타내는 순서도.Figure 2 is a flow chart showing a method for advanced treatment of sewage using a conventional sequencing batch reactor (Sequencing Batch Reactor).
도 3은 일반적인 흡입식 중공사막 활성 슬러지 방법에 사용되는 시스템의 개략도.3 is a schematic diagram of a system used in a general suction hollow fiber membrane activated sludge method.
도 4는 본 발명을 이용한 파일럿 실험에서의 운전방식 및 주기 추적 연구 (Cycle Study) 결과: 반응조내의 질산화 및 탈질화 양상.FIG. 4 shows the results of operation and cycle study in a pilot experiment using the present invention: nitrification and denitrification in a reactor. FIG.
상기 설명한 바와 같이, 본 발명은 흡입식 중공사막을 이용하는 막활성 슬러지 방법에 있어서, 반응조 원액을 직접 고액 분리하여 처리수를 뽑아내는 폐수처리 방법에서, 폭기 단계 및 무산소단계를 동일한 단일 반응조내에서 교차시킴으로써 질산화 및 탈질화 반응을 유도하여 하수중 질소 처리를 촉진하는 것을 특징으로 하는 폐수처리 방법에 관한 것이다.As described above, the present invention is a membrane activated sludge method using a suction hollow fiber membrane, in the wastewater treatment method in which the reaction solution is directly solid-liquid separated to extract the treated water, and the aeration step and the anaerobic step are crossed in the same single reactor. The present invention relates to a wastewater treatment method characterized by inducing nitrification and denitrification reactions to promote nitrogen treatment in sewage.
또한, 본 발명은 원수유입, 폭기, 막여과가 동시에 이루어졌던 기존의 막 활성 슬러지 방법의 운전방식 대신 원수유입, 무산소, 혼합, 폭기, 막 여과의 5가지 공정을 적절히 조합 또는 연결함으로써 질소 제거에 필요한 탈질화 및 질산화 공정이 동일한 단일 반응조내에서 이루어질 수 있도록 한 것을 특징으로 한다.In addition, the present invention, instead of the operation method of the conventional membrane activated sludge method in which raw water inflow, aeration, and membrane filtration were simultaneously performed, appropriately combines or connects five processes of raw water inflow, oxygen-free, mixing, aeration, and membrane filtration to remove nitrogen. It is characterized in that the necessary denitrification and nitrification processes can be carried out in the same single reactor.
본 발명의 간헐폭기식 막 활성 슬러지법에 의하면 전체 공정은 크게 무산소 단계 및 폭기 단계의 두 단계로 이루어져 있다. 각 단계에 있어서의 세부적인 공정내용은 다음과 같다.According to the intermittent aeration membrane activated sludge method of the present invention, the entire process consists of two stages, an anoxic stage and an aeration stage. The detailed process contents in each step are as follows.
(1) 무산소 단계 (도 4 참조)(1) anoxic stage (see Figure 4)
본 단계에서는 반응조로의 산소폭기가 중단되면서 동시에 수중펌프에 의한 무산소 혼합 (anoxic mixing)과 원수유입이 이루어지게 된다. 산소 농도가 떨어지면 탈질화에 필요한 제반 조건, 즉 무산소 조건 (anoxic condition)과 탈질화 미생물을 위한 기질 (substrate) 확보, 또 수중펌프에 의한 적절한 교반 등의 조건들이 갖추어지게 되어 수중 질산화물에 대한 탈질화 반응이 본격적으로 일어나게 된다. 본 단계에서 일어나는 주요 반응을 처리 대상 물질로 구분하여 요약하면 다음과 같다.In this step, oxygen aeration into the reactor is stopped and at the same time, anoxic mixing and inflow of raw water are performed by an underwater pump. When the oxygen concentration drops, the conditions necessary for denitrification, such as anoxic conditions, securing a substrate for denitrifying microorganisms, and proper agitation by an underwater pump, are established. The reaction takes place in earnest. The main reactions occurring in this step can be summarized as follows.
- 질산성 질소 (NO2-N, NO3-N): 탈질화 미생물에 의해 N2가스로 전환되어 제거된다.Nitrate nitrogen (NO 2 -N, NO 3 -N): converted to N 2 gas by denitrifying microorganisms and removed.
- 유기물: 탈질화 미생물에 의해 소모되며 생분해성이 낮은 유기물은 대부분 보존된다.-Organics: Consumed by denitrifying microorganisms, most biodegradable organics are preserved.
- 유기 질소 및 암모니아성 질소: 유기질소 중 일부가 암모니아로 변환되며 암모니아성 질소는 원수 중에 보존된다.Organic nitrogen and ammonia nitrogen: Some of the organic nitrogen is converted to ammonia and ammonia nitrogen is preserved in raw water.
(2) 폭기 단계(2) aeration stage
폭기 단계에서는 반응조로의 폭기가 시작되면서 흡입 펌프에 의한 막여과가 시작된다. 이때 산기 장치에서 발생되는 공기방울은 두 가지 중요한 역할을 갖게 되는데 하나는 반응조의 산소 농도를 높여 폭기조건을 만들어주는 것이며 다른 하나는 수면으로 올라오는 과정에서 발생되는 와류로 막폐색을 억제하는 역할이다. 따라서, 산기관을 막모듈 하단부에 위치시키는 것이 바람직하며, 발생기포에 의한 상향 수류가 막모듈면적을 충분히 포함할 수 있도록 배치한다. 발생 기포 크기도 충분한 상향 수류를 일으킬 수 있도록 적절한 크기로 조절해주는 것이 바람직하다.In the aeration stage, aeration into the reactor starts and membrane filtration by the suction pump begins. At this time, the air bubbles generated from the air diffuser have two important roles. One is to create an aeration condition by increasing the oxygen concentration in the reactor, and the other is to suppress membrane blockage due to the vortices generated during the process. . Therefore, it is preferable to place the diffuser at the lower end of the membrane module, so that the upstream water flow generated by the generation bubbles sufficiently includes the membrane module area. It is desirable to adjust the size of the generated bubble to an appropriate size so as to cause sufficient upward flow.
흡입에 의한 막여과는 간헐적으로 운전되는데 이는 흡입이 중단되는 시간동안 공기방울이 발생시키는 상향 수류를 이용하여 막세척 효과를 반복함으로써 장기적으로 막폐색 경향을 최대한 억제할 수 있기 때문이다.Membrane filtration by inhalation is operated intermittently because the tendency of membrane occlusion can be suppressed as long as possible by repeating the membrane cleaning effect by using the upstream water flow generated by air bubbles during the inhalation period.
폭기 단계에서 일어나는 주요 반응을 요약하면 다음과 같다.A summary of the main reactions occurring in the aeration phase follows.
- 질산성 질소(NO2-N, NO3-N): 보존되거나 부분적인 탈질화가 일어난다.Nitrate nitrogen (NO 2 -N, NO 3 -N): Conserved or partial denitrification occurs.
- 유기물 (BOD, COD) 제거: 원수 유입과 더불어 유입된 유기물 중 무산소 단계에서 분해되지 않은 잔류 유기물의 분해가 일어난다.Removal of organic matter (BOD, COD): With the introduction of raw water, decomposition of undecomposed residual organic matter occurs in the anoxic phase of the introduced organic matter.
- 유기질소 및 암모니아성 질소: 암모니아성 질소가 질산성 질소로 변화되며, 이후 유기 질소의 질산화가 진행된다.Organic nitrogen and ammonia nitrogen: Ammonia nitrogen is converted to nitrate nitrogen, followed by nitrification of organic nitrogen.
본 공정에 있어서는 여타의 막활성 슬러지법과 마찬가지로 슬러지 (반응 미생물) 발생량이 최소화되기 때문에 일주일 또는 그 이상의 주기로 슬러지를 폐기해 주며 운전 사이클에 있어서의 폐기 시점은 폭기단계의 마지막 시점이 바람직하다.In this process, sludge (reactive microorganisms) is minimized like other membrane activated sludge methods, and thus, sludge is disposed of in a week or more cycle. The disposal point in the operation cycle is preferably at the end of the aeration stage.
본 발명의 방법에 있어서 또 다른 특징은 한 사이클내의 여러 가지 공정 수행 시간을 적절한 시간 프로그램에 따라 조절 수행하는 것이며 이때 시간 프로그램은 PLC (programｍable logic control)를 이용하여 손쉽게 조절할 수 있다는 것이다. 즉, 무산소 단계와 폭기 단계의 상대적인 시간 간격을 손쉽게 조절할 수 있어 다양한 원수의 성상에 대해 효과적으로 대응할 수 있게 된다. 예를 들어, 원수의 C:N 비가 낮을 경우에는 운전사이클 시간을 늘리고 무산소 단계의 시간을 늘려줌으로써 충분한 탈질화를 달성할 수 있으며 반대로 C:N 비가 높은 경우에는 운전 사이클 시간을 줄임으로써 처리 용량을 극대화 할 수 있다.Another feature of the method of the present invention is that various process execution times in one cycle are adjusted according to an appropriate time program, wherein the time program can be easily adjusted using programmable logic control (PLC). That is, the relative time interval between the anaerobic stage and the aeration stage can be easily adjusted to effectively cope with the characteristics of various raw water. For example, when the C: N ratio of raw water is low, sufficient denitrification can be achieved by increasing the operating cycle time and by increasing the anoxic phase time, while reducing the operating cycle time by reducing the operating cycle time when the C: N ratio is high. Can be maximized.
즉, C:N 비가 높은 주방 또는 식당 폐수 처리에서는 무산소 단계/폭기 단계의 시간비를 1:1.5 내지 1:2 정도로 하되 운전 사이클 시간을 2 시간 이내로 하는 것이 바람직하다. 한편, 합병 정화조 유출수와 같이 C:N 비가 낮은 경우에는 시간비를 1:0.5 내지 1:1 범위로 하되, 운전 사이클은 2 시간 내지 3 시간 정도로 길게 잡아 탈질화를 위한 충분한 시간을 확보하는 것이 필요하다.That is, in a kitchen or restaurant wastewater treatment having a high C: N ratio, it is preferable that the time ratio of the anaerobic stage / aeration stage is about 1: 1.5 to 1: 2 but the operating cycle time is within 2 hours. On the other hand, when the C: N ratio is low, such as the combined septic tank effluent, the time ratio should be in the range of 1: 0.5 to 1: 1, but the operating cycle should be long enough for 2 to 3 hours to ensure sufficient time for denitrification. Do.
본 발명의 방법에 있어서, 일반적으로 원수 유입 시기는 특별한 제한은 없으나, 폭기 단계후 산소농도가 충분히 감소된 후에 집중되는 것이 바람직하다. 이는 유입원수중에 함유된 탄소원을 탈질화 반응에 최대한 활용할 수 있기 때문이다.In the method of the present invention, in general, the raw water inflow timing is not particularly limited, but is preferably concentrated after the oxygen concentration is sufficiently reduced after the aeration step. This is because the carbon source contained in the influent can be utilized to the denitrification reaction to the maximum.
한편, 본 발명을 이용한 파일럿 실험에서의 운전방식 및 주기 추적 연구(Cycle Study) 결과를 반응조내의 질산화 및 탈질화 양상으로 도 4에 나타내었다.On the other hand, the operation method and cycle tracking (Cycle Study) results in the pilot experiment using the present invention is shown in Figure 4 as the nitrification and denitrification in the reactor.
도 4에서 알 수 있는 바와 같이, 폭기가 시작되면, 질산화가 진행되면서 암모니아 농도가 감소하게 되고, 약 10 분정도 지나면 완전히 제거된다. 따라서, 폭기 단계가 시작된 후 흡입에 의한 막분리를 동시에 진행하지 않고 일정시간 유보한 후에 진행하게 되면 처리수 중 암모니아 농도를 추가적으로 낮추는 효과를 얻을 수 있다. 이러한 흡입을 유보함으로써 막분리가 유보되는 시간동안에는 막에 압력이 걸리지 않는 상태에서 폭기된 공기방울이 막을 스치면서 지나가기 때문에 막이 세정되는 부수적인 효과도 얻을 수 있다.As can be seen in Figure 4, when aeration begins, ammonia concentration decreases as nitrification proceeds, and after about 10 minutes, it is completely removed. Therefore, if the aeration step is started after a certain period of time without proceeding the membrane separation by suction at the same time it can be obtained to further lower the ammonia concentration in the treated water. By retaining this inhalation, a side effect of cleaning the membrane can be obtained because the aerated bubbles pass through the membrane while the membrane separation is under no pressure.
<실시예><Example>
도 3에 나타낸 장치를 사용하여 본 발명에 의한 폐수처리 방법과 종래의 중공사막 활성 슬러지법에 의한 폐수처리 방법을 비교하였다. 파일럿 규모 실험 (일 10톤처리)으로, 종래의 중공사막 활성 슬러지법에 따른 방법의 경우 원수의 연속유입, 반응조의 연속 폭기방식에 의해서 수행하였으며, 본원 발명에 따른 폐수처리 방법은 도 4에 나타낸 바와 같이, 폭기 단계 및 무산소 단계 시간을 각각 30 분으로 하는 간헐 유입, 간헐 폭기식으로 운전하였다. 그 결과에 따른 본 발명에 의한 처리법과 기존의 막활성 슬러지법 (연속유입, 연속폭기)의 처리효율을 비교하여 표 2에 나타내었다.The wastewater treatment method according to the present invention and the wastewater treatment method by the conventional hollow fiber membrane activated sludge method were compared using the apparatus shown in FIG. In the pilot scale experiment (10 tons per day), the method according to the conventional hollow fiber membrane activated sludge method was carried out by the continuous inflow of raw water, the continuous aeration method of the reactor, the wastewater treatment method according to the present invention is shown in FIG. As described above, the operation was performed in an intermittent inflow and intermittent aeration manner in which the aeration stage and the anaerobic stage time were 30 minutes, respectively. Table 2 compares the treatment efficiency of the present invention and the conventional membrane activated sludge method (continuous inflow, continuous aeration) according to the results.
본 발명의 운전방식에 따라 하수를 처리함으로써, 고 부하처리, 부하변동과 상관없는 안정적 수질확보, 슬러지 발생량 저감 등의 막활성 슬러지법의 장점을 살리면서 추가적으로 하수 중 질소를 효과적으로 제거할 수 있는 하수 처리방법이 제공된다.By treating the sewage according to the operation method of the present invention, sewage which can effectively remove nitrogen from the sewage while taking advantage of the membrane active sludge method such as high load treatment, ensuring stable water quality independent of load fluctuation, and reducing sludge generation amount A treatment method is provided.
Claims (4)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1019990012626A KR100327151B1 (en) | 1999-04-10 | 1999-04-10 | A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1019990012626A KR100327151B1 (en) | 1999-04-10 | 1999-04-10 | A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| KR20000065883A KR20000065883A (en) | 2000-11-15 |
| KR100327151B1 true KR100327151B1 (en) | 2002-03-13 |
Family
ID=19579306
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| KR1019990012626A KR100327151B1 (en) | 1999-04-10 | 1999-04-10 | A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor |
Country Status (1)
| Country | Link |
|---|---|
| KR (1) | KR100327151B1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020011791A (en) * | 2000-08-04 | 2002-02-09 | 강인중 | Membrane coupled sequencing batch apparatus for separation |
| KR100685411B1 (en) | 2005-09-26 | 2007-02-22 | (주)이엔이 | Apparatus for treating wastewater using membrane |
| CN108911136A (en) * | 2018-07-17 | 2018-11-30 | 厦门理工学院 | A kind of processing method of heavy metal wastewater thereby |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100435621B1 (en) * | 2002-08-24 | 2004-06-12 | 효림산업주식회사 | A advance sewage treatment plant system |
| KR20020094950A (en) * | 2002-12-02 | 2002-12-18 | 쌍용양회공업(주) | Method and apparatus for wastewater treatments |
| KR101328008B1 (en) | 2012-11-05 | 2013-11-13 | 한국과학기술연구원 | Apparatus and method for anaerobic wastewater treatment with membrane |
| KR101667931B1 (en) | 2014-02-14 | 2016-10-21 | 한국과학기술연구원 | Apparatus and method for anaerobic wastewater treatment with fluidized media membrane distillation |
| KR101667932B1 (en) | 2014-02-14 | 2016-10-21 | 한국과학기술연구원 | Apparatus and method for anaerobic wastewater treatment with membrane distillation |
| KR20160148197A (en) | 2015-06-16 | 2016-12-26 | 한국과학기술연구원 | Submerged anaerobic membrane bioreactor and method for wastewater treatment using the same |
| KR101788574B1 (en) | 2015-06-19 | 2017-11-15 | 한국과학기술연구원 | Submerged anaerobic membrane bioreactor |
| CN106115896A (en) * | 2016-06-22 | 2016-11-16 | 南京瑞洁特膜分离科技有限公司 | A kind of modularity nitration denitrification membrane bioreactor |
| CN108911134B (en) * | 2018-07-17 | 2021-06-11 | 厦门理工学院 | Domestic sewage treatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06262173A (en) * | 1993-03-15 | 1994-09-20 | Daicel Chem Ind Ltd | Membrane purifying method for surface water with improved recovery rate and operation method of its device |
| JPH0768294A (en) * | 1993-09-06 | 1995-03-14 | Kubota Corp | Wastewater treatment method |
| JPH07256251A (en) * | 1994-03-18 | 1995-10-09 | Chlorine Eng Corp Ltd | Rotational belt-type oil recovering apparatus |
| JPH09192688A (en) * | 1996-01-17 | 1997-07-29 | Hitachi Chem Co Ltd | Method for intermittently aerating sewage |
| JPH10277550A (en) * | 1997-04-10 | 1998-10-20 | Mitsubishi Rayon Co Ltd | Sludge thickening method and sludge thickening system |
-
1999
- 1999-04-10 KR KR1019990012626A patent/KR100327151B1/en not_active IP Right Cessation
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06262173A (en) * | 1993-03-15 | 1994-09-20 | Daicel Chem Ind Ltd | Membrane purifying method for surface water with improved recovery rate and operation method of its device |
| JPH0768294A (en) * | 1993-09-06 | 1995-03-14 | Kubota Corp | Wastewater treatment method |
| JPH07256251A (en) * | 1994-03-18 | 1995-10-09 | Chlorine Eng Corp Ltd | Rotational belt-type oil recovering apparatus |
| JPH09192688A (en) * | 1996-01-17 | 1997-07-29 | Hitachi Chem Co Ltd | Method for intermittently aerating sewage |
| JPH10277550A (en) * | 1997-04-10 | 1998-10-20 | Mitsubishi Rayon Co Ltd | Sludge thickening method and sludge thickening system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020011791A (en) * | 2000-08-04 | 2002-02-09 | 강인중 | Membrane coupled sequencing batch apparatus for separation |
| KR100685411B1 (en) | 2005-09-26 | 2007-02-22 | (주)이엔이 | Apparatus for treating wastewater using membrane |
| CN108911136A (en) * | 2018-07-17 | 2018-11-30 | 厦门理工学院 | A kind of processing method of heavy metal wastewater thereby |
Also Published As
| Publication number | Publication date |
|---|---|
| KR20000065883A (en) | 2000-11-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7172699B1 (en) | Energy efficient wastewater treatment for nitrogen and phosphorus removal | |
| KR100412330B1 (en) | Membrane Coupled Activated Sludge Method Operating Anoxic/Anaerobic Zone alternatively for Removal of Nitrogen and Phosphorus | |
| JP4632356B2 (en) | Biological nitrogen removal method and system | |
| AU2007238520A1 (en) | Method and system for nitrifying and denitrifying wastewater | |
| KR101721251B1 (en) | SBR Process coupled with Membrane Process | |
| KR100327151B1 (en) | A Process for Treatment of Wastewater Using Intermittently Aerated Membrane Bioreactor | |
| KR100422211B1 (en) | Management Unit and Method of Foul and Waste Water | |
| CN110054361A (en) | A kind of electric field-enhanced MBR sewage treatment process | |
| EP1346956A1 (en) | Process for sludge treatment using sludge pretreatment and membrane bioreactor | |
| KR101326402B1 (en) | Membrane Bio Reactor system comprising Sequencing Batch Reactor and method using the same | |
| KR100479649B1 (en) | The procces and apparatus of Livestock wastewater treatment. | |
| KR20040075413A (en) | Wastewater treatment system by multiple sequencing batch reactor and its operation methods | |
| JPS58210897A (en) | Biological dephosphorization method of waste water | |
| KR100555689B1 (en) | Wastewater treatment by influent controlled membrane bioreactor | |
| KR101828296B1 (en) | Wastewater Processing Appliance using Existing Activated Sludge Appliance as Shortcut Nitrogen Removal Process | |
| KR100435107B1 (en) | Advance Treatment Equipment and Process for Nitrogen and Phosphate Removal in Sewage and Wastewater | |
| CN1350985A (en) | Method for biochemically treating wastewater | |
| KR20010076873A (en) | Organic and nitrogen compound removal methods from landfill leachate using an anaerobic-aerobic-anoxic system | |
| KR19990083645A (en) | Organic material and nitrogen, phosphate removal method using intermitted aeration process and plate type microfiltration membrane | |
| KR20020089085A (en) | Apparatus for treating Nitrogen and Phosphorus in wastewater and A Treatment method thereof | |
| KR100416693B1 (en) | Method for removing nutrients of domestic sewage using 2 step aeration and an apparatus used therefor | |
| JP2002233889A (en) | Method of removing nitrogen or phosphorus in waste water | |
| KR19990030405A (en) | Wastewater Purification Using Distribution Inflow | |
| KR200289075Y1 (en) | Apparatus of Livestock wastewater treatment. | |
| KR100504150B1 (en) | Method for sewage and wastewater treatment using anaerobic batch reactor and hybrid sequencing batch reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A201 | Request for examination | ||
| E902 | Notification of reason for refusal | ||
| E701 | Decision to grant or registration of patent right | ||
| GRNT | Written decision to grant | ||
| FPAY | Annual fee payment |
Payment date: 20090130 Year of fee payment: 8 |
|
| LAPS | Lapse due to unpaid annual fee |