KR101005422B1 - Apparatus and method for high flux membrane wastewater treatment using early stage control of membrane fouling - Google Patents

Apparatus and method for high flux membrane wastewater treatment using early stage control of membrane fouling Download PDF

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KR101005422B1
KR101005422B1 KR20080082110A KR20080082110A KR101005422B1 KR 101005422 B1 KR101005422 B1 KR 101005422B1 KR 20080082110 A KR20080082110 A KR 20080082110A KR 20080082110 A KR20080082110 A KR 20080082110A KR 101005422 B1 KR101005422 B1 KR 101005422B1
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membrane
filtration
backwash
submerged
change
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KR20100023383A (en )
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김관엽
김형수
나유미
이억재
이의종
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주식회사 엔텍
주식회사 태영건설
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D65/00Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02Membrane cleaning or sterilisation ; Membrane regeneration
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D61/00Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis, ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14Ultrafiltration; Microfiltration
    • B01D61/18Apparatus therefor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D61/00Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis, ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14Ultrafiltration; Microfiltration
    • B01D61/22Controlling or regulating
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • C02F3/12Activated sludge processes
    • C02F3/1236Particular type of activated sludge installations
    • C02F3/1268Membrane bioreactor systems
    • C02F3/1273Submerged membrane bioreactors
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2315/00Details relating to the membrane module operation
    • B01D2315/06Submerged-type; Immersion type
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2321/00Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/04Backflushing
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2321/00Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/12Use of permeate
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2321/00Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/16Use of chemical agents
    • B01D2321/168Use of other chemical agents
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00Controlling or monitoring parameters in water treatment
    • C02F2209/005Processes using a programmable logic controller [PLC]
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00Controlling or monitoring parameters in water treatment
    • C02F2209/03Pressure
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00Specific treatment goals
    • C02F2303/16Regeneration of sorbents, filters
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage
    • Y02W10/15Aerobic processes

Abstract

본 발명은 하폐수 처리장치 및 방법에 관한 것으로, 침지형막에 의하여 처리수를 생산하고, 침지형막의 막오염 초기에 자동제어를 통한 약품역세척을 실시하여 고플럭스로 여과하는 초기막오염제어를 이용한 막여과 하폐수 처리장치 및 처리방법을 제공한다. The invention wastewater processing apparatus and to a method, produces treated by an immersion type membrane, the membrane and subjected to cleaning reagents station through the automatic control in an immersion type membrane fouling initial Using initial film pollution control filtration in flux filtration provides a wastewater processing apparatus and processing method. 여기서 자동제어를 통한 약품역세척은 침지형막의 막간차압으로부터 산출한 순간차압변화율을 산정한 후, 산출된 순간차압변화율이 일정하면 약품역세척없이 여과를 계속하고, 산출된 순간차압변화율이 급격히 변화하면 초기 막오염물질을 제거하기 위해 약품역세척하는 방법을 말한다. The agent backwashing through the automatic control is if you a moment after the differential pressure calculating the rate of change, the calculated moment the differential pressure rate of change calculated from the immersion type membrane transmembrane pressure difference constant continue the filtration without the agent backwashing, and the moment when the differential pressure rate of change rapidly changes calculated It refers to a method for agent backwashing to remove the initial film contamination. 본 발명에 따르면 막오염을 초기에 효율적으로 제어하여 여과성능을 향상시키고, 이를 통하여 막사용량 및 막여과에 필요한 부대설비를 1/2로 감소시킬 수 있다. According to the invention the film and contamination by the initial efficiently controlled to improve the filtration performance, it is possible to reduce the film use and film bag equipment necessary to filtration through it to 1/2.
막분리, 막오염, 약품역세척, 초기 막오염 제어, 순간차압변화율, 고플럭스 Membrane separation, membrane fouling, chemicals backwash, initial film pollution control, the moment the differential pressure rate of change, a high flux

Description

초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치 및 처리방법{Apparatus and method for high flux membrane wastewater treatment using early stage control of membrane fouling} Initial film and using a pollution control flux membrane filtration wastewater processing apparatus and a processing method {Apparatus and method for high flux membrane wastewater treatment using early stage control of membrane fouling}

본 발명은 하폐수 처리장치 및 처리방법에 관한 것으로, 보다 상세하게는 막오염을 초기에 효율적으로 제어하여 여과성능을 향상시킬 수 있는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치 및 처리방법에 관한 것이다. The present invention relates to a wastewater processing apparatus and processing method, and more particularly, film-effective to improve filtering performance initial film and using a pollution control flux membrane filtration wastewater processing apparatus and a processing method to control the contamination in the initial It relates.

막여과 활성슬러지 공법은 분리막으로 고액분리를 완벽히 수행하고 생물 반응조 내에 고농도의 미생물을 유지함으로써 안정적인 처리수질을 얻을 수 있고, 생물 반응조의 부피를 현저히 감소시킬 수 있으며 자동운전이 가능한 장점이 있다. Membrane filtering the activated sludge process can obtain a stable quality of the treated water by completely performing the solid-liquid separation by the separation membrane and maintains a high concentration of microorganisms in a bioreactor, can significantly reduce the volume of the bioreactor, and the advantage is automatic operation possible.

그러나 이러한 다양한 장점에도 불구하고 상용화가 어려운 이유는 분리막사용에 과다한 초기투자비용 및 에너지 비용 그리고 분리막의 오염에 따른 막의 세정 및 교체때문이다. However, these various reasons, even though commercialized is difficult advantage is that the membrane cleaning and replacement of the excessive pollution of the initial investment costs and energy costs and the membrane used in the membrane. 따라서 분리막사용을 최소화하기 위해 막면적당 생산되는 처리수량(플럭스,ℓ/㎡/h)을 증가시키기 위한 노력을 하고 있으나 플럭스 증가에 따라 막오염 속도가 증가하기 때문에 막여과 활성슬러지법은 적정한 플럭스, 소위 임계플럭스(critical flux)이하에서 운전해야 하는 단점이 있다. Therefore, the separation membrane in order to minimize the use of processing produced a film coating quantity (flux, ℓ / ㎡ / h) efforts to increase and but because the increase in membrane fouling rate in accordance with the flux increasing membrane filtration activated sludge process is suitable flux, so-called would have to remember to operation below the critical flux (critical flux). PVDF재질의 중공사 막(hollow fiber membrane)을 사용한 대부분 막여과 활성슬러지 공법에서는 안정적인 여과성능을 유지하기 위하여 20ℓ/㎡/h의 플럭스를 채택하고 있다. Most membrane filtration activated sludge method using a hollow fiber membrane (hollow fiber membrane) of the PVDF material adopts a flux of 20ℓ / ㎡ / h to maintain a stable filtration performance.

임계플럭스 이하로 막여과를 실시하면 분리막의 오염은 서서히 진행되어 여과성능이 안정되게 유지되나 어느 시점에 도달하면 막오염이 급격히 진행되어 여과성능의 급격한 변화를 가져온다. When subjected to membrane filtration to less than the critical flux contamination of the membrane is gradually proceeding filtration performance stably maintained but when reaching a certain point in time is fouling progresses rapidly resulting in a sharp change in the filtration performance. 따라서 이러한 변화를 막기 위해 역세척시 화학약품을 첨가하여 유지세정(maintenance cleaning)을 주기적으로 실시하고 있으나 이를 위해 별도의 약품역세척펌프를 사용하고 있고 이 경우에도 임계플럭스 이상으로 막여과를 실시하지 못하고 있다. Therefore, cleaning maintenance by the addition of chemicals for cleaning station in order to prevent this change (maintenance cleaning) to, but conducted periodically and to use a separate drug backwash pump for this purpose in this case to carry out membrane filtration to the critical flux than It is not.

이러한 문제점을 해결하기 위한 방안으로서, 본 발명의 목적은 막오염 진행 초기에 막오염 성분을 효과적으로 제거하여 임계플럭스 이상의 고플럭스 막여과 운전을 하기 위한 것이다. As measures to solve these problems, an object of the present invention to a critical flux and flux over the membrane filtration operation to effectively remove membrane contaminants in progress fouling early.

본 발명의 다른 목적은 종래보다 막여과 활성슬러지 공법보다 2배 높은 40ℓ/㎡/hr의 고플럭스로 막여과를 하여 막사용량 및 막여과에 필요한 밸브, 흡입펌프, 블로워 등과 같은 부대설비의 사용량을 1/2로 감소시키기 위한 것이다. It is another object of the present invention the amount of incidental facilities, such as membrane filtration activated sludge method than twice the 40ℓ / ㎡ / hr of a high valve by the membrane filtration to the flux necessary for the film usage and membrane filtration, the suction pump, the blower than the conventional It is to reduce to 1/2.

이러한 목적들을 달성하기 위하여, 본 발명은 침지형막이 설치된 막여과 활성슬러지장치와, 여과역세척장치를 포함하는 하폐수 처리장치를 제공한다. In order to achieve these objects, the present invention provides a wastewater treatment device comprising a membrane filtration unit with activated sludge, filter backwash immersion type membrane unit is installed. 상기 여과역세척장치는 처리수 저장탱크, 역세척약품펌프, 자동밸브, 압력계 및 자동제어장치를 포함하여 구성된다. The filtration backwash device is configured to include a process water storage tank, a backwash drug pump, automatic valves, pressure gauge and automatic control devices. 상기 처리수 저장탱크는 흡입여과시에 상기 침지형막에서 여과된 처리수를 저장한다. The treated water storage tank stores the treated water filtered by the submerged membrane at the time of suction filtration. 상기 역세척약품펌프는 약품역세척시에 역세척라인으로 역세척약품을 공급한다. The backwash drug pump supplies reverse cleaning reagents by the backwash line upon agent backwashing. 상기 자동밸브는 상기 침지형막과 상기 처리수 저장탱크 사이의 처리수의 흐름 방향을 조절한다. The automatic valve controls the flow direction of the treated water between the submerged membrane and the treated water storage tanks. 상기 압력계는 상기 침지형막의 막간차압을 측정한다. The pressure gauge measures the transmembrane pressure difference the immersion type membrane. 그리고 상기 자동제어장치는 상기 측정된 막간차압을 이용하여 순간차압변화율을 산출하고, 상기 산출된 순간차압변화율이 일정하면, 여과를 계속하고, 상기 산출된 순간차압변화율이 급격히 변화하면, 상기 자동밸브를 제어하여 상기 처리수 저장탱크의 처리수를 상기 침지형막으로 보내되, 상기 처리수에 상기 역세척약품을 혼합하여 상기 침지형막으로 보내는 약품역세척을 실시하게 한다. And the automatic control unit when calculating the rate of change pressure differential moment using the measured transmembrane pressure difference, and is the calculated time differential pressure rate of change constant, Continuing the filtration, wherein the rapidly changing moment the differential pressure change rate calculation, the automatic valve to be sent to the submerged membrane to treated water in the treated water storage tank is controlled, by mixing the backwash drugs to be the processing to be carried the agent backwashing sent to the submerged membrane.

본 발명은 상기의 고플럭스 막여과 하폐수 처리장치의 하폐수 처리방법을 제공한다. The present invention provides a wastewater treatment method of the high-flux membrane filtration wastewater treatment device. 본 발명에 따른 하폐수 처리방법은 상기 침지형막에 의하여 오염물질을 여과하는 단계와, 상기 침지형막의 막간차압으로부터 산출한 순간차압변화율을 산정하는 단계와, 상기 산출된 순간차압변화율이 일정하면, 여과를 계속하는 단계와, 상기 산출된 순간차압변화율이 급격히 변화하면, 상기 자동밸브를 제어하여 상기 처리수 저장탱크의 처리수를 상기 침지형막으로 보내되, 상기 처리수에 상기 역세척약품을 혼합하여 상기 침지형막으로 주입하고, 막오염 물질을 용해시켜 제거하기 위해 일정 시간동안 정치하는 단계를 포함하여 구성된다. When the wastewater treatment process according to the invention; and a step of estimating a moment the differential pressure rate of change calculated from the immersion type membrane transmembrane pressure difference, the calculated moment the differential pressure rate of change for filtering contaminants by the submerged membrane constant, the filtering the mixture of the reverse cleaning reagents to keep step and, when the rapidly changing the calculated instantaneous differential pressure change ratio, being sent to control the automatic valve for the treatment of the process water storage tank to the submerged membrane, can be the treatment of injected into the submerged membrane, and the membrane to dissolve the contaminants comprises the step of standing for a certain period of time to remove.

본 발명의 초기막오염동제어를 이용한 고플럭스 막여과 하폐수처리방법은 초기에 막오염 성분을 제거하여 고플럭스 막여과를 실시할 수 있으므로 막사용량 및 막여과에 필요한 압력계, 흡입펌프, 블로워, 밸브 등의 사용량을 1/2로 감소시킨다. Initial Fouling move the using high flux membrane filtration control of the present invention, wastewater treatment method can be subjected to filtration and to remove the membrane contaminants initially flux film required for film usage and membrane filtration pressure gauge, suction pump, a blower, a valve It reduces the amount of such as one-half.

또한, 여과시 흡입하는 여과펌프와 약품역세척시 역세척용액을 공급하는 역세척펌프를 별도로 설치하지 않고 동일한 펌프를 사용하므로 설치 및 유지관리가 용이하고 경제적이다. In addition, the installation without a backwash pump for supplying a backwash filter pump and the drug during the backwash solution when the suction filtered separately using the same pump, the installation and maintenance easy and economical so.

이하, 본 발명을 첨부된 도면에 의하여 상세히 설명한다. It will now be described in detail by the accompanying drawings, the present invention.

도 1은 본 발명의 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장 치의 개략적인 구성을 나타낸 도면으로, 본 발명의 하폐수 처리장치는 침지형 막분리 활성슬러지장치(100)와 여과역세척장치(200)를 포함하여 구성된다. 1 is a view showing a schematic configuration values ​​and using the initial film pollution control of the present invention the flux membrane filtration wastewater treatment, wastewater treatment device according to the present invention is filtered off and the immersion type membrane separation activated sludge unit 100 includes a backwash device (200 ) it is configured to include a.

침지형 막여과 활성슬러지장치(100)는 혐기조(111), 무산소조(112) 및 막분리 호기조(113)를 구비하고 있다. Submerged membrane filtration activated sludge unit 100 includes an anaerobic tank 111, an anoxic tank 112 and a membrane separation aerobic tank 113. 혐기조(111)로 유입된 원수는 무산소조(112)를 지나 막분리 호기조(113)로 유입된다. The raw water flowing into the anaerobic tank 111 flows into through the anoxic tank 112, membrane separation aerobic tank 113. 또한 막분리 호기조(113)내 슬러지는 제1슬러지 반송장치(130)에 의해 무산소조(112)로 반송되고, 무산소조(112) 내 슬러지는 제2슬러지 반송장치(140)에 의해 혐기조(111)로 반송된다. In addition to the anaerobic tank 111 by the membrane separation aerobic tank 113 is within the sludge first is conveyed to the anoxic tank 112 by the sludge conveying device (130), the anoxic tank 112 is within the sludge of the second sludge return unit 140 It is conveyed.

여기서 혐기조(111)에서는 미생물에서 인 성분이 방출된다. Wherein the anaerobic tank 111 is discharged are in the microbial components. 무산소조(112)에서는 질산성질소가 질소가스로 환원되어 질소가 제거된다. Anoxic tank 112, the nitrogen is removed nitrate nitrogen is reduced to nitrogen gas. 그리고 막분리 호기조(113)에서는 유입수 중 암모니아성 질소가 질산성질소로 산화되고, 유입수 중 인 성분이 미생물에 의해 과잉섭취되고, 유입수 중 유기물 성분이 미생물에 의해 산화되어 제거된다. And the membrane separation aerobic tank 113, and the ammonium nitrogen of the incoming water oxidation Thoreau nitrate, the influent of a component being ingested over by microorganisms, the organic components of the incoming water is removed is oxidized by microorganisms. 막분리 호기조(113)에서 미생물에 의해 과잉섭취된 인 성분은 슬러지 배출펌프(150)에 의해 배출된 슬러지 내 미생물에 포함되어 제거된다. Ingredients the membrane separation aerobic tank intake 113 over by microorganisms is removed from the microorganisms contained in the sludge discharged by the sludge discharge pump 150.

막분리 호기조(113) 외측 하부에는 슬러지를 간헐적으로 배출하는 슬러지 배출펌프(150)가 설치되어 있다. Membrane separation aerobic tank 113, the outer bottom has a sludge discharge pump 150 for intermittently discharging sludge is installed in. 막분리 호기조(113)의 내부에는 여과운전시 고형물을 걸러주는 침지형막(114)이 설치되어 있다. Inside the membrane separation aerobic tank 113 has a submerged membrane 114 to filter out the solids during filtration operation is provided. 또한 여과운전에 의해 걸러진 고형물이 침지형막(114)에 부착되는 것을 방지하기 위해 침지형막(114) 하부에 제1산기장치(115)가 설치되어 있다. There is also a first diffuser 115, the lower submerged membrane 114 in order to prevent the solids filtered by the filtering operation that is attached to the submerged membrane 114 is installed. 막분리 호기조(113) 내 미생물 생장에 필요한 산소를 공급하기 위해 제2산기장치(116)가 설치되어 있다. Film and a second air diffuser (116) is provided for separation aerobic tank 113, supplying oxygen necessary for microbial growth. 제1산기장치(115) 및 제2산기장치(116)에 공기를 공급하도록 막분리 호기조(113)의 외부에는 공기공급장치(120)가 설치되어 있다. Claim 1 has a diffuser 115 and the second air diffuser (116) to the outside, the air supply apparatus 120 of the membrane separation aerobic tank 113 to supply the air is provided.

여과역세척장치(200)는 여과역세척펌프(430), 압력계(260) 및 자동제어장치(250)를 포함하여 구성된다. Filtered backwashing device 200 is configured to include a filter backwash pump 430, a pressure gauge 260 and the automatic control unit (250). 그리고 여과와 약품역세척 방향을 조절하는 자동밸브(210, 220, 230, 240), 처리수 저장탱크(310) 및 역세척약품펌프(420)가 있고, 역세척약품은 역세척약품 탱크(410)에 저장되어 있다. And an automatic valve (210, 220, 230, 240), the process can be a storage tank 310 and a backwash drug pump 420 for controlling the three way filter and drug station, and a backwash agent is backwash medicine tank (410 ) it is stored in.

여과역세척펌프(430)는 침지형막(114)의 여과운전시에는 처리수를 흡입하여 처리수 저장탱크(310)로 보내고, 약품역세척시에는 처리수 저장탱크(310)의 처리수를 침지형막(114)으로 주입한다. Filtered backwash pump 430 is submerged for treatment of an immersion type membrane when sending the number of the process during the filtration operation to the suction process storage tank 310 by, agent backwashing of 114, the treated water storage tank 310 the film implanted with 114. 종래의 막여과 활성슬러지법에서는 여과시 흡입하는 여과펌프와 역세척시의 약품역세척펌프를 별도로 설치하였으나, 본 발명에서는 여과역세척 펌프(430)를 여과와 약품역세척에 함께 사용한다. In the conventional activated sludge process of membrane filtration installation, but the drug backwash pump during filtration and backwashing pump to suction during filtering separately, the present invention uses the filter backwash pumps 430, along with the filtered drug backwash.

압력계(260)는 분리막의 막간차압을 측정하고, 자동제어장치(250)는 압력계(260)에서 측정한 막간차압을 전송받아 순간차압변화율을 산정하고 여과시와 약품역세척시에 역세척약품펌프(420) 및 자동밸브(210, 220, 230, 240)의 운전 및 개폐를 제어하는 기능을 수행한다. Pressure gauge 260 may measure the transmembrane pressure difference of the separator, and the automatic control unit 250 is washed estimate the instantaneous differential pressure rate of change take a transmembrane pressure difference measured in the pressure gauge 260 is transmitted to the station at the time of cleaning filtration with chemicals station drug pump 420 and performs a function of controlling the operation and the shut-off of automatic valve (210, 220, 230, 240). 자동밸브(210, 220, 230, 240)는 4개로 구성되어 있다. Automatic valve (210, 220, 230, 240) is composed of four. 제1자동밸브(210)는 여과시 처리수가 여과역세척 펌프(430)로 이송되도록 흐름을 제어한다. The first automatic valve 210 controls the flow to be transferred to be processed with filtered filtration backwash pump 430. 제2자동밸브(220)는 여과시 여과역세척 펌프(430)를 지나 처리수 저장탱크(310)로 이송되도록 흐름을 제어한다. The second automatic valve 220 controls the flow to be filtered through the filter during the backwash pump 430 is transferred to the process water storage tank 310. 제3자동밸브(230)는 약품역세척시 처리수 저장탱크(310)에 저장된 처리수가 여과역세척 펌프(430)로 이송되도록 흐름을 제어한다. The third automatic valve 230 controls the flow so that the treatment water transferred to the filter backwash pump 430 is stored in the storage tank 310 can be processed with agent backwashing. 그리고 제4자동밸브(240)는 약품역세척시 처리수 저장탱크(310)에 저장된 처리수가 여과역세척 펌프(430)를 지나 침지형막(114)으로 공급되도록 흐름을 제어한다. And the fourth automatic valve 240 controls the flow to be filtered through the treated water backwash pump 430 is stored in the treated water upon agent backwashing storage tank (310) supplied to the submerged membrane 114.

이하에서는 도 2 내지 도 4를 참조하여 본 발명에 따른 초기막오염 제어를 이용한 막여과 하폐수 처리방법을 설명한다. In reference now to FIGS. 2 to 4 will be described in the initial film membrane filtration wastewater treatment method using a pollution control according to the present invention.

먼저 침지형막(114)에 의하여 처리수를 생산하는 여과 단계(S11)를 거친다. First subjected to a filtering step (S11) of producing the treated water by the submerged membrane 114. 즉 도 2는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치의 여과 단계를 나타낸 것으로, 제1자동밸브(210) 및 제2자동밸브(220)가 열리고, 제3자동밸브(230) 및 제4자동밸브(240)가 닫힘으로써 여과라인(300)을 형성한다. That is, FIG. 2 is high using the initial film pollution control showing a filtration step of the flux membrane filtration wastewater treatment device, a first automatic valve 210 and the second open and the automatic valve 220, the third automatic valve 230 and the fourth automatic valve 240 is closed as to form the filtered line 300.

침지형 막여과 활성슬러지장치(100)의 혐기조(111)로 유입된 원수는 무산소조(112)를 지나고 막분리 호기조(113)로 유입된다. The raw water flowing into the anaerobic tank 111 of the submerged membrane filtration activated sludge unit 100 is passed to the anoxic tank 112 is introduced into the membrane separation aerobic tank 113. 막분리 호기조(113) 내 슬러지는 제1슬러지 반송장치(130)에 의해 무산소조(112)로 반송되고, 무산소조(112) 내 슬러지는 제2슬러지 반송장치(140)에 의해 혐기조(111)로 반송된다. Membrane separation aerobic tank 113, sludge is conveyed to the anoxic tank 112 by the first sludge return unit 130 and sludge anoxic tank 112 is returned to the anaerobic tank 111 by means of a second sludge return unit 140 do.

또한 막분리 호기조(113) 내의 고형물은 여과시 침지형막(114)의 표면에서 걸러지고, 정화된 처리수만 분리막 내로 유입되게 된다. In addition, solids in the membrane separation aerobic tank 113 are filtered at the surface of the submerged membrane filtration unit 114, only the purification process is to be introduced into the separator. 이 때 상기 침지형막(114)의 표면에 붙은 고형물은 공기공급장치(120)로부터 공급된 공기가 침지형막(114) 하부에 설치된 제1산기장치(115)를 통해 공기방울 형태로 상승하면서 털어줌으로써 제거된다. At this time, by giving off the submerged frozen solid to the surface of the film 114 and rise to the air bubbles form through a first diffuser 115, the air supplied from the air supply apparatus 120 is installed on the lower submerged membrane 114 It is removed.

다음으로, 침지형막(114)의 막간차압으로부터 산출한 순간차압변화율을 산정한다(S12). Next, calculate the moment the differential pressure rate of change calculated from the transmembrane pressure difference of the submerged membrane (114) (S12).

S12단계의 산정결과 순간차압변화율이 일정하면, 여과단계인 S11단계를 계속해서 수행한다. When the calculation result of the instantaneous differential pressure change rate constant step S12, and continues to perform the filtering step of S11 step.

반면, S12단계의 비교결과 막간차압으로부터 산출한 순간차압변화율이 급격히 변화하면 침지형막(114)을 약품역세척한다(S14). On the other hand, if for a moment the differential pressure rate of change calculated from the transmembrane pressure difference of the result of the comparison step S12 is rapidly changing and washing the submerged membrane 114 drug station (S14). 여기서 약품역세척은 자동제어장치(250)가 압력계(260)에서 감지되는 막간차압을 전송받아 순간차압변화율(ΔP/ΔT), 즉 막오염 속도를 산출하여 각 자동밸브(210, 220, 230, 240)의 개폐를 제어함으로써 여과운전의 역방향으로 처리수와 역세척약품이 혼합된 역세척용액을 침지형막(114)으로 보내는 것으로 실시된다. The drug backwash automatically control device 250 is a differential pressure moment take a transmembrane pressure difference that is detected by the pressure gauge 260, transmission rate of change (ΔP / ΔT), i.e., each of the automatic valve (210, 220, 230 and the film yield contamination rate, by controlling the opening and closing of the 240) is performed by sending a reverse treated with backwash drug when mixed backwash solution to the filtering operation of the submerged membrane 114. the

도 3은 본 발명의 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치의 약품역세척 단계를 나타낸 것으로, 제1자동밸브(210) 및 제2자동밸브(220)는 닫히고, 제3자동밸브(230) 및 제4자동밸브(240)가 열림으로써 역세척 라인(400)을 형성한다. Figure 3 is closed and shows an initial film drugs backwash phase of the flux membrane filtration wastewater treatment unit and with pollution control of the present invention, the first automatic valve 210 and the second automatic valve 220, the third automatic valve 230, and a fourth as the automatic valve 240 is opened to form a backwash line (400).

여과역세척 펌프(430)에 의해 처리수 저장탱크(310)의 처리수가 역세척 라인(400)으로 공급되고, 이는 소정의 위치에서 역세척약품펌프(420)를 통해 주입되는 역세척약품과 혼합된다. Filter backwash and not processing of the wastewater storage tank 310 by a pump 430 supplied to the backwash line 400, which back washing chemicals and mix injected through the cleaning reagents pump 420 station in the predetermined position do. 이렇게 혼합된 역세척용액을 일정시간 침지형막(114)으로 주입하여 역세척함으로써 분리막 표면 또는 내부에 부착된 가역적인 막오염 물질을 떼어낸다. Thus injecting the mixed backwash solution to the submerged membrane predetermined time 114 to Detach the reversible membrane contaminants attached to the membrane surface or by internal cleaning station. 역세척 후에는 자동제어장치(250)의 신호에 의해 모든 자동밸브(210, 220, 230, 240)가 닫히고, 여과역세척 펌프(430)도 운전이 중지되어 침지형막(114) 내부에 역세척용액이 채워진 상태로 일정시간 정치된다. After backwashing is closed and all the automatic valves (210, 220, 230, 240) by a signal of the automatic control device 250, the filtered backwash pump 430 is also stopped driving backwashed therein submerged membrane 114 is a predetermined time value to the solution the filled state. 이는 비가역적인 막오염 물질을 역세척용액의 화학작용으로 용해시켜 제거하기 위한 것이다. This is to remove by dissolving the non-reversible membrane contaminants by chemical action of the backwash solution.

이러한 약품역세척을 함으로써 종래의 화학세정보다 저농도의 약품으로 단시간 내에 막오염 성분을 제거하게 되고, 고플럭스(40ℓ/㎡/hr)에서도 안정적인 막여 과 운전이 지속될 수 있다. By these medications backwash it is to remove the membrane contaminants in a short period of time with a low concentration of drug than conventional chemical cleaning, a high flux (40ℓ / ㎡ / hr) in a stable makyeo and operation can continue.

역세척약품으로는 침지형막(114)의 세정에 유효한 것이라면 어떠한 약품을 사용하여도 무방하다. Back washing with chemicals is also mubang using any drug so long effective for cleaning the submerged membrane 114. 바람직하게는 차아염소산나트륨(NaOCl)을 사용하는 것이다. Preferably is the use of sodium hypochlorite (NaOCl). 이는 경제적이면서도 막여과 활성슬러지법에서의 침지형막(114)의 세정에 효율적인 것으로 알려져 있기 때문이다. This is because economical and efficient filtration membrane known cleaning of activated sludge submerged membrane 114 in.

상기 일련의 약품역세척이 종료되면 침지형막(114)의 여과성능이 회복되고, 다시 상기 여과운전이 재개된다(S11). When the series of drug backwashing is completed the filtration performance of the submerged membrane 114 it is recovered, and the filtering operation is resumed (S11).

약품역세척시 처리수량은 침지형막(114)의 형태 및 크기에 따라 다른데, 막 모듈당 10~40 L를 사용하고, 처리수와 역세척약품이 혼합된 역세척용액은 차아염소산나트륨으로 0.01 ~ 0.06 %의 농도로 실시한다. When agent backwashing process quantity differs depending on the shape and size of the submerged membrane 114, the membrane using 10 ~ 40 L per module, and the process number and the reverse cleaning reagents are mixed backwash solution to the same procedure as set forth in 0.01 carried out at a concentration of 0.06%. 상기 역세척용액의 농도가 0.01 % 미만이면 세정 효과가 떨어지고, 0.06 % 초과이면 역세척용액의 사용량의 증가로 인해 경제적 부담이 커지는 문제점이 있다. The concentration of the backwash solution is less than 0.01%, the cleaning effect is poor, if more than 0.06%, there is a problem due to the large increase in the economic burden of the amount of backwash solution.

약품역세척시, 역세척용액 주입시간은 2~5분, 역세척플럭스는 여과시와 동일한 40ℓ/㎡/hr으로 하고, 정치시간은 30~60분으로 하는데, 시간은 작업 상황 등에 따라 조정 가능하다. When agent backwashing, backwash solution injection time can be 2 ~ 5 minutes, the backwash flux is the same 40ℓ / ㎡ / hr and during filtration, political time for 30 to 60 minutes, the time is adjusted according to the working conditions Do.

본 명세서에 기재된 실시예와 도면에 의해 본 발명은 한정되지 않으며, 본 발명이 속하는 기술 분야에서 당업자에 의해 다양한 변경이 가능할 것이다. Embodiment the present invention by examples and figures disclosed herein is not limited, it will be modified in various ways by those skilled in the art.

본 발명은 막오염 초기에 약품역세척으로 막을 처음상태로 되돌림으로써, 여과효율이 향상되어 40ℓ/㎡/hr 이상의 높은 플럭스로 운전이 가능하게 한다. The invention film by returning the film to the initial contamination agent backwashing in the first state, the filtering efficiency is improved to enable the driver to 40ℓ / ㎡ / hr or more high flux.

또한, 여과역세척 펌프를 여과와 약품역세척에 함께 사용할 수 있고, 역세척 라인 내에서 역세척약품과 처리수를 혼합함으로써 별도의 역세척용액 탱크를 설치할 필요가 없으므로 장치의 경제성을 향상시킬 수 있다. Further, the filter backwash pump for use with filtration and drug backwashing, by mixing a backwash drug and processed in the backwash line because there is no need to install a separate backwash solution tank to improve the economical efficiency of the device have.

도 1은 본 발명의 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치의 개략적인 구성을 나타낸 도면 1 is a diagram showing a general configuration of a membrane filtration flux wastewater treatment apparatus and using the initial film pollution control of the present invention

도 2는 본 발명의 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치의 여과단계를 나타낸 도면 Figure 2 is a view of the initial membrane filtration step in membrane filtration flux wastewater treatment unit and with pollution control of the present invention

도 3은 본 발명의 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치의 약품역세척 단계를 나타낸 도면 Figure 3 is a view of the initial film drugs backwash phase of the membrane filtration flux wastewater treatment unit and with pollution control of the present invention

도 4는 본 발명의 실시예에 따른 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리방법을 보여주는 흐름도 Figure 4 is a flow diagram showing the initial membrane flux membrane filtration wastewater treatment method and with the pollution control according to an embodiment of the present invention

** 도면의 주요 부분에 대한 부호의 설명 ** Description of the drawings ** **

100 : 활성슬러지장치 110 : 교반기 100: activated sludge unit 110: stirrer

111 : 혐기조 112 : 무산소조 111: anaerobic tank 112: anoxic

113 : 막분리 호기조 114 : 침지형막 113: membrane separation aerobic tank 114: Submerged Membrane

115 : 제1산기장치 116 : 제2산기장치 115: a first diffuser 116: the second air diffuser

120 : 공기공급장치 130 : 제1슬러지 반송장치 120: air supply apparatus 130: a first sludge return unit

140 : 제2슬러지 반송장치 150 : 슬러지 배출펌프 140: second sludge return unit 150: sludge discharge pump

200 : 여과역세척장치 210 : 제1자동밸브 200: Filtration backwashing device 210: first automatic valve

220 : 제2자동밸브 230 : 제3자동밸브 220: second automatic valve 230: the third automatic valve

240 : 제4자동밸브 250 : 자동제어장치 240: a fourth automatic valve 250: servomechanisms

260 : 압력계 300 : 여과라인 260: 300 Pressure gauge: filtration lines

310 : 처리수 저장탱크 400 : 역세척 라인 310: process water storage tank 400: backwash line

410 : 역세척약품 탱크 420 : 역세척약품펌프 410: backwash tank 420 drug: drug backwash pump

430 : 여과역세척 펌프 430: filter backwash pump

Claims (5)

  1. 침지형막이 설치된 막여과 활성슬러지장치와, 여과역세척장치를 포함하는 하폐수 처리장치에 있어서, In the activated sludge and the membrane filtration device, an immersion type membrane installed, the wastewater treatment apparatus including a filter backwash device,
    상기 여과역세척장치는, The filtration backwash device,
    흡입여과시에 상기 침지형막에서 여과된 처리수가 저장되는 처리수 저장탱크와; At the time of suction filtration and the treated water storage tank which stores the number of filtering processing in the immersion type membrane;
    약품역세척시에 역세척라인으로 역세척약품을 공급하는 역세척약품펌프와; Backwash drug pump for supplying a backwash with the backwash line drugs during the agent backwashing;
    상기 침지형막과 상기 처리수 저장탱크 사이의 처리수의 흐름 방향을 조절하는 자동밸브와; And automatic valves for controlling the direction of flow of the treated water between the submerged membrane and the treated water storage tank;
    상기 침지형막의 막간차압을 측정하는 압력계와; And a pressure gauge measuring the submerged membrane transmembrane pressure difference;
    상기 측정된 막간차압을 이용하여 순간차압변화율을 산출하고, 상기 산출된 순간차압변화율이 일정하면, 여과를 계속하고, 상기 산출된 순간차압변화율이 급격히 변화하면, 상기 자동밸브를 제어하여 상기 처리수 저장탱크의 처리수를 상기 침지형막으로 보내되, 상기 처리수에 상기 역세척약품을 혼합하여 상기 침지형막으로 보내는 약품역세척을 실시하게 하는 자동제어장치;를 포함하며, Calculating the rate of change pressure differential moment by using the measured transmembrane pressure difference, and when said calculated instantaneous differential pressure rate of change constant, Continuing the filtration, the rapidly changing the calculated moment the differential pressure rate of change, can the processing to control the automatic valve It is sent to the submerged membrane to treated water storage tank of the automatic control apparatus for a mixture of the reverse cleaning reagents to be subjected to the treatment agent backwashing sent to the submerged membrane; includes,
    상기 침지형막이 PVDF재질의 중공사막(hollow fiber membrane)일 경우 고플럭스(40ℓ/㎡/h)로 여과하는 것을 특징으로 하는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치. The submerged hollow fiber membrane of PVDF material (hollow fiber membrane) days for high flux (40ℓ / ㎡ / h) initial film high flux membrane filtration wastewater treatment apparatus using a pollution control, comprising a step of filtration with.
  2. 제1항에 있어서, According to claim 1,
    처리수와 역세척약품이 혼합된 역세척용액의 차아염소산나트륨(NaOCl)의 농도는 0.01 ~ 0.06 % 인 것을 특징으로 하는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리장치. Treated with backwash drug when mixed backwash sodium hypochlorite (NaOCl) concentrations from 0.01 to 0.06 percent of the initial membrane flux and membrane filtration wastewater treatment apparatus using a pollution control, comprising a step of solution.
  3. 삭제 delete
  4. 제1 또는 제2항에 따른 막여과 하폐수 처리장치의 하폐수 처리방법에 있어서, The method of claim 1 or the wastewater treatment method of membrane filtration wastewater treatment device according to claim 2,
    상기 침지형막에 의하여 오염물질을 여과하는 단계; The step of filtering the pollutant by the submerged membrane;
    상기 침지형막의 막간차압으로부터 산출한 순간차압변화율을 산정하는 단계; The step of estimating a moment the differential pressure rate of change calculated from the immersion type membrane transmembrane pressure difference;
    상기 산출된 순간차압변화율이 일정하면, 여과를 계속하는 단계; When the calculated instantaneous differential pressure rate of change constant, the method comprising continuing the filtration;
    상기 산출된 순간차압변화율이 급격히 변화하면, 상기 자동밸브를 제어하여 상기 처리수 저장탱크의 처리수를 상기 침지형막으로 보내되, 상기 처리수에 상기 역세척약품을 혼합하여 상기 침지형막으로 주입하고, 막오염 물질을 용해시켜 제거하기 위해 일정 시간동안 정치하는 단계;를 포함하며, When the calculated instantaneous differential pressure rate of change rapidly changes, it is sent to control the automatic valve for the treatment of the process water storage tank to the submerged membrane, a mixture of the reverse cleaning reagents to be the process and injected into the submerged membrane comprising the steps of: standing for a certain period of time to remove the film by dissolving the contaminants; includes,
    상기 침지형막이 PVDF재질의 중공사막(hollow fiber membrane)일 경우 고플럭스(40ℓ/㎡/h)로 여과하는 것을 특징으로 하는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리방법. The submerged hollow fiber membrane of PVDF material (hollow fiber membrane) days for high flux (40ℓ / ㎡ / h) initial film high flux membrane filtration wastewater treatment method using a pollution control, comprising a step of filtration with.
  5. 제4항에 있어서, 5. The method of claim 4,
    상기 약품역세척하는 단계는, 상기 처리수에 상기 역세척약품을 혼합하여 상기 침지형막으로 2~5분간 여과시와 같은 고플럭스로 침지형막에 주입하고, 막오염 물질을 용해시켜 제거하기 위해 30~60분 동안 정치하는 단계를 포함하는 것을 특징으로 하는 초기막오염제어를 이용한 고플럭스 막여과 하폐수 처리방법. The drug backwash step to 30 to remove, by mixing the backwash drugs to be the process by the submerged membrane with a high flux, such as during 2-5 minutes, filtered and injected into the submerged membrane, followed by film dissolution contaminants to 60 minutes and the initial membrane flux membrane filtration wastewater treatment method using a pollution control, comprising a step of standing for.
KR20080082110A 2008-08-21 2008-08-21 Apparatus and method for high flux membrane wastewater treatment using early stage control of membrane fouling KR101005422B1 (en)

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