KR20040093960A - Wastewater microfiltration apparatus with metal membrane combined ozonated water back-washing - Google Patents
Wastewater microfiltration apparatus with metal membrane combined ozonated water back-washing Download PDFInfo
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- KR20040093960A KR20040093960A KR1020030027846A KR20030027846A KR20040093960A KR 20040093960 A KR20040093960 A KR 20040093960A KR 1020030027846 A KR1020030027846 A KR 1020030027846A KR 20030027846 A KR20030027846 A KR 20030027846A KR 20040093960 A KR20040093960 A KR 20040093960A
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- membrane module
- water
- filtration
- dissolved ozone
- ozone water
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- 239000012528 membrane Substances 0.000 title claims abstract description 119
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 239000002184 metal Substances 0.000 title claims abstract description 31
- 229910052751 metal Inorganic materials 0.000 title claims abstract description 31
- 239000002351 wastewater Substances 0.000 title claims abstract description 16
- 238000011001 backwashing Methods 0.000 title claims abstract description 13
- 238000001471 micro-filtration Methods 0.000 title 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 91
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 239000010802 sludge Substances 0.000 claims abstract description 6
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 238000001914 filtration Methods 0.000 claims description 69
- 238000004140 cleaning Methods 0.000 claims description 35
- 238000000034 method Methods 0.000 claims description 31
- 239000007789 gas Substances 0.000 claims description 17
- 238000002347 injection Methods 0.000 claims description 17
- 239000007924 injection Substances 0.000 claims description 17
- 229910001220 stainless steel Inorganic materials 0.000 claims description 7
- 239000010935 stainless steel Substances 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 238000000151 deposition Methods 0.000 claims description 3
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 3
- 239000010931 gold Substances 0.000 claims description 3
- 229910052737 gold Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 3
- 239000000706 filtrate Substances 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 abstract 2
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 239000010865 sewage Substances 0.000 abstract 1
- 239000000126 substance Substances 0.000 description 18
- 238000005406 washing Methods 0.000 description 12
- 230000000694 effects Effects 0.000 description 11
- 238000011084 recovery Methods 0.000 description 11
- 239000000243 solution Substances 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 229910019093 NaOCl Inorganic materials 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 238000000967 suction filtration Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 208000035859 Drug effect increased Diseases 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000004792 oxidative damage Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D39/00—Filtering material for liquid or gaseous fluids
- B01D39/10—Filter screens essentially made of metal
- B01D39/12—Filter screens essentially made of metal of wire gauze; of knitted wire; of expanded metal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
- B01D29/66—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps
- B01D29/68—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps with backwash arms, shoes or nozzles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/88—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices
- B01D29/90—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for feeding
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/06—Flat membranes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/10—Preparation of ozone
- C01B13/11—Preparation of ozone by electric discharge
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/78—Details relating to ozone treatment devices
- C02F2201/782—Ozone generators
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Textile Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
본 발명은 반응조내에 내산화성을 지닌 금속여과막 모듈을 침적시킨 막분리장치를 이용한 오·폐수 처리시스템에 관한 것으로, 특히 오존수를 이용한 간헐적 역세정방식을 도입함으로써 운용의 간편성을 도모함과 동시에, 기존의 막분리 시스템에 존재하는 막투과유속의 저하와 세정에 따른 운용관리의 번잡성을 해결할 수 있고 처리효율을 극대화할 수 있는 용존오존수 주입 역세정 방법을 이용한 오·폐수 정밀여과장치에 관한 것이다.The present invention relates to a wastewater treatment system using a membrane separation device in which a metal filtration membrane module having oxidation resistance is deposited in a reaction tank, and in particular, by introducing an intermittent backwashing method using ozone water, the operation is simplified, and The present invention relates to a wastewater fine filtration system using a dissolved ozone water injection backwash method that can solve the complexity of operation management due to the decrease of membrane permeation flow rate and cleaning present in the membrane separation system and maximize the treatment efficiency.
최근 막분리기술의 진전과 함께 막을 이용한 고액분리법에 의한 오·폐수의 고도처리 또는 처리수의 수자원으로서의 재이용에 관한 연구가 활발히 진행되고 있다.Recently, with the advance of membrane separation technology, researches are being actively conducted on the advanced treatment of wastewater and wastewater by the solid-liquid separation method using membranes or the reuse of treated water as water resources.
막분리 방식은 처리과정에서 발생되는 슬러지(sludge)의 침강성에 처리성능이 좌우되지 않고 안정한 처리수질을 확보할 수 있으며, 최종침전지가 불필요하므로 처리 소요면적을 절감할 수 있는 장점을 지니고 있다.Membrane separation method has the advantage of reducing the processing area because the treatment performance is not dependent on the sedimentation of sludge generated in the treatment process, and the stable treatment water quality can be obtained.
그러나, 상기 막분리방식은 이러한 장점을 지니고 있음에도 불구하고, 실제 막분리방식을 적용함에 있어서, 시간의 경과에 따라 여과막이 열화되고, 내부 파울링(fouling)에 의한 막투과 유속이 저하되는 문제점을 내포하고 있다. 이러한 문제점은 오·폐수처리 분야에 있어 좀더 광범위한 막분리 장치를 적용하는데 걸림돌로 작용하고 있으며, 이에 따라 안정된 막투과 유속의 유지 및 막수명의 연장을 실현시키기 위한 방안이 모색되고 있다.However, although the membrane separation method has such an advantage, in applying the actual membrane separation method, the membrane is deteriorated with time, and the membrane permeation flow rate due to internal fouling is lowered. It is implicated. This problem acts as an obstacle to applying a wider range of membrane separation devices in the field of wastewater treatment. Accordingly, a plan for achieving stable membrane permeation flow rate and extension of membrane life has been sought.
막투과 유속의 저하를 방지하기 위해 지금까지 여과막모듈의 하부로부터 공기폭기를 수행하여 역세정을 하는 물리학적 세정방법이나, 약액을 이용한 화학적 세정방법등을 채용하고 있는 실정이다. 그러나, 상기 공기폭기를 이용한 단순한 물리적 세정방법은 시간의 경과에 따라 그 세정효과가 감소하고, 막투과유속의 회복을 위한 효과가 지속적이고 충분하지 못할 뿐만 아니라, 세정하기 위해 여과막을 반응조로부터 도출하는데 소요되는 시간과, 그에 따른 시스템의 운전을 정지해야 하는 문제점을 내포하고 있다. 또한, 상기 약액을 이용한 화학적 세정방법은 약액의 보충과 그 농도 조정을 빈번히 행해야 하고, 세정후의 여과막에 잔류하는 약액세정액을 추가로 처리해야 하는 등 운영관리상의 번잡성이 따르며, 화학적인 약액을 이용할 경우 여과막 내부의 오염으로 인한 역효과가 발생하는 문제점이 있다.In order to prevent a decrease in the membrane permeation flow rate, a physical cleaning method for backwashing by performing an air aeration from the lower part of the filtration membrane module or a chemical cleaning method using a chemical solution has been adopted. However, the simple physical cleaning method using the air aeration reduces the cleaning effect over time, the effect for the recovery of the membrane permeation flow rate is not continuous and sufficient, and the filtration membrane is removed from the reaction tank for cleaning. There is a problem in that the time required and the system must be stopped accordingly. In addition, the chemical cleaning method using the chemical solution is often complicated in operation management, such as supplementing the chemical solution and adjusting its concentration frequently, and additionally treating the chemical liquid cleaning solution remaining in the filtration membrane after washing, and using a chemical chemical solution. In this case, there is a problem that adverse effects occur due to contamination inside the filtration membrane.
이들 물리 ·화학적 세정방법이 가지고 있는 문제점을 해소하기 위하여 본원발명의 출원인은 국내 공개특허공보 제 2002 - 0086806 호의 『간헐적 오존주입 역세정 방법을 이용한 금속막 오폐수 고도처리장치 및 방법』을 제안한 바 있으며, 이 기술에서는 상기의 물리 · 화학적 방법이 가지고 있는 문제점을 해결하였다.In order to solve the problems of these physical and chemical cleaning methods, the applicant of the present invention has proposed `` Metal film wastewater advanced treatment apparatus and method using intermittent ozone injection backwashing method '' of Korean Patent Publication No. 2002-0086806. This technique solves the problems of the above physical and chemical methods.
그러나, 상기의 오존가스를 이용한 세정방법은 가스를 이용하여 세정을 하기 때문에, 막표면에 부착된 미세한 공기방울에 의해 여과막 표면적에 여과기능을 발휘하지 못하는 사공간(dead space)이 발생되어 막투과 유속의 회복을 저하시킬 수 있는 문제점이 있다.However, in the cleaning method using ozone gas, the cleaning is performed by using gas, so that dead spaces that do not exhibit the filtration function on the surface area of the filtration membrane are generated by minute air bubbles adhering to the membrane surface. There is a problem that can lower the recovery of the flow rate.
따라서, 본 발명은 상기의 제반문제점을 해결하기 위하여 제안된 것으로서, 공기나 약액에 의한 세정방법 대신에 산화력이 강한 오존가스를 막여과수에 용해시키고, 오존이 용해된 여과수를 막모듈의 내부에 간헐적으로 주입하여 내부 파울링현상 및 막표면에 케익층(Cake layer)이 형성되는 것을 방지하여 항시 높은 막투과유속의 유지를 도모할 수 있고, 원수에 침적시킨 금속여과막 모듈의 내부압력을 여과막 모듈 외부의 압력보다 작게한 흡인 여과방식을 사용하여 고액분리가 가능하도록 한 용존오존수 주입 역세정 방법을 이용한 오·폐수 정밀여과장치를 제공함에 그 목적이 있다.Accordingly, the present invention has been proposed to solve the above problems, and instead of the cleaning method by air or chemical liquid, ozone gas having strong oxidizing power is dissolved in the membrane filtered water, and the filtered water in which ozone is dissolved is intermittently inside the membrane module. It is possible to prevent the fouling phenomenon and the formation of cake layer on the membrane surface by injecting it into the membrane to maintain high membrane permeation flow rate at all times, and the internal pressure of the metal filtration membrane module deposited in raw water It is an object of the present invention to provide a wastewater precision filtration system using a dissolved ozone water injection backwashing method that enables solid-liquid separation using a suction filtration method smaller than the pressure of.
또한, 본 발명은 여과막을 내오존성 소재인 금속막으로 제조함으로써 기존의 여과막으로 사용되고 있는 수지막(유기성재질막)으로는 적용이 불가능한 오존수의 적용을 가능케 함과 동시에 막의 수명을 거의 반영구적으로 연장시킬 수 있는 용존오존수 주입 역세정 방법을 이용한 오·폐수 정밀여과장치를 제공함에 다른 목적이 있다.In addition, the present invention enables the application of ozone water, which is not applicable to the resin membrane (organic material membrane) which is used as a conventional filtration membrane by manufacturing the filtration membrane as a metal membrane which is an ozone-resistant material, and at the same time, extends the membrane life almost semi-permanently. It is another object to provide a wastewater precision filtration apparatus using a dissolved ozone water injection backwash method.
도1은 본 발명에 따른 용존오존수 주입 역세정 방법을 이용한 오·폐수 정밀여과장치의 일실시예 구성을 나타낸 개략적인 모식도.Figure 1 is a schematic diagram showing the configuration of an embodiment of the wastewater precision filtration apparatus using the dissolved ozone water injection backwashing method according to the present invention.
도2는 본 발명의 요부인 금속 여과막 모듈의 구성을 나타낸 사시도.Figure 2 is a perspective view showing the configuration of a metal filtration membrane module that is the main portion of the present invention.
도3은 각 조작인자에 따른 세정을 실시하였을 경우의 막투과유속의 비(Javerage/Jinitial)를 나타낸 그래프도.3 is a graph showing the ratio (J average / J initial ) of the membrane permeation flow rate when the washing is performed according to each operation factor.
* 도면의 주요부분에 대한 부호의 설명** Explanation of symbols for the main parts of the drawings *
1 : 반응조 2 : 금속막 모듈1: reactor 2: metal film module
3 : 유입원수 4 : 여과수3: inflow water 4: filtered water
5 : 흡인관 6 : 흡인 펌프5: suction pipe 6: suction pump
7 : 용존오존수 주입장치 8 : 분리판7: Dissolved ozone water injection device 8: Separator
9 : 금속막 10 : 여과틀체9: metal film 10: filter frame
11 : 흡인구 12 : 용존오존수 주입구11 suction port 12 dissolved ozone water inlet
21: 분출노즐 22: 공급관로21: blowoff nozzle 22: supply line
상기 목적을 달성하기 위하여 본 발명은, 외부로부터 유입된 원수를 수용하며, 슬러지를 침적시키기 위한 공간을 제공하는 반응조; 상기 반응조내부의 소정위치에 침적되며, 그에 수용된 원수를 통과시켜 고액분리하는 여과막모듈; 일단이 상기 여과막 모듈의 상부에 연결되어 그를 통과하는 여과수를 강제흡인하여 배출하며, 상기 여과막 모듈 내부를 부압으로 유지시켜 여과수의 고액 분리가 행해지도록 하기 위한 여과수 흡인수단; 상기 여과막 모듈의 하부에 장착되며, 용존 오존수를 상측으로 분출시켜 여과막 모듈의 막세정을 수행하는 용존오존수 분출수단; 및 상기 용존 오존수 분출수단에 연결되며, 오존가스를 여과수에 용해시킨 용존 오존수를 용존 오존수 분출수단에 주입하는 용존오존수 주입수단을 포함하는 용존오존수 주입 역세정 방법을 이용한 금속막 오·폐수 정밀여과장치를 제공한다.In order to achieve the above object, the present invention, the reaction vessel for receiving the raw water introduced from the outside, and provides a space for depositing the sludge; A filtration membrane module which is deposited at a predetermined position in the reaction tank, and passes through raw water contained therein to separate solid-liquid; Filtration water suction means for one end is connected to the upper portion of the filtration membrane module forcibly sucked out the filtered water passing through it, to maintain the inside of the filtration membrane module at a negative pressure so that the solid-liquid separation of the filtered water is performed; Dissolved ozone water jetting means mounted on the lower portion of the filtration membrane module, and discharges the dissolved ozone water to the upper side to perform the membrane cleaning of the filtration membrane module; And dissolved ozone water injection means connected to the dissolved ozone water jetting means and including dissolved ozone water injection means for injecting dissolved ozone water dissolved in filtered water into the dissolved ozone water jetting means. To provide.
상기와 같이 구성된 본 발명에서, 상기 반응조는 그의 내부 저면과 소정거리 떨어진 위치에 직립되게 설치되어 외부로부터 공급되는 원수의 하강류가 형성되도록 하여 원활한 유동성을 가지도록 하기 위한 분리판을 더 포함한다.In the present invention configured as described above, the reaction tank further includes a separation plate to be installed upright at a position away from the inner bottom surface thereof to have a smooth flow by forming a downflow of raw water supplied from the outside.
또한, 상기 여과수 모듈은 상면에 투과수 흡인수단과 연결되는 흡인구가 설치되고, 하단부에는 용존오존수 분출수단과 연결되는 분출구가 구비되며, 양측면이 개방된 틀체와; 상기 틀체의 양측면에 설치되는 금속막을 포함한다.In addition, the filtered water module is provided with a suction port connected to the permeate suction means on the upper surface, the lower end is provided with a discharge port connected to the dissolved ozone water jetting means, the frame body with both sides open; It includes a metal film provided on both sides of the frame.
상기 금속막은 유효여과면적이 양면합계 0.12m2이고, 막공경은 0.2μm 이다. 또한, 상기 금속막은 스테인레스강의 금망에 스테인레스강의 분말을 도포하여 소결한 것이다.The metal membrane has an effective filtration area of 0.12 m 2 on both sides and a membrane pore diameter of 0.2 μm. The metal film is sintered by applying a powder of stainless steel to a gold mesh of stainless steel.
상기 용존오존수 주입수단은 플라즈마에 의해 공기중의 산소를 오존으로 변환시키고, 고압을 이용해 상기 오존가스를 여과수에 용해시키는 플라즈마 장치를 포함한다.The dissolved ozone water injection means includes a plasma device that converts oxygen in the air into ozone by plasma, and dissolves the ozone gas in the filtered water by using a high pressure.
상기 여과수 흡인수단은 여과막 모듈의 흡인구에 연결된 배출관과; 상기 배출관상에 설치되어 상기 여과막모듈 내부로 유입되는 여과수를 강제 흡인하는 흡인펌프를 포함한다.The filtered water suction means and the discharge pipe connected to the suction port of the filter membrane module; And a suction pump installed on the discharge pipe to forcibly suck the filtered water introduced into the filtration membrane module.
이하, 첨부된 도면을 참조하여 본 발명의 실시예를 상세히 설명한다.Hereinafter, with reference to the accompanying drawings will be described an embodiment of the present invention;
본 발명에 의한 금속막을 이용한 오·폐수 정밀여과장치는 오존가스를 여과수에 용해시킨 용존 오존수를 금속막에 투입하여 막세정을 효율적으로 수행하기 위해 구현된 것으로, 본 발명의 실시예에서는 도1에 도시된 바와 같이, 외부로부터 유입된 원수(3)를 수용하여 슬러지를 침적시키기 위한 공간을 제공하는 반응조(1)와; 상기 반응조(1)의 내부 중앙에 설치되며, 저면과 소정거리만큼 이격되게 직립되어 원수(3)가 원활하게 유동되도록 하기 위한 분리판(8)과; 상기 분리판(8)의 일측, 즉 원수(3)가 유입되는 방향의 반대측 공간에 설치되어 상승하는 원수(3)를 통과시켜 고액분리를 행하는 여과막 모듈(2)과; 일단이 상기 여과막 모듈(2)의 상부에 설치되어 그를 통과한 여과수(4)를 흡인 ·배출하는 경로를 제공하는 흡인관(5)과; 상기 흡인관(5)의 소정위치에 설치되며, 상기 여과막 모듈(2)을 통과하는 여과수(4)를 강제흡인하여 배출하되, 상기 여과막 모듈(2) 내부를 부압으로 유지시켜 여과수(4)의 고액 분리가 행해지도록 하기 위한 흡인펌프(6)와; 상기 여과막 모듈(2)의 하부에 장착되며, 용존 오존수를 상측으로 분출시켜 여과막 모듈(2)의 막세정을 수행하는 분출노즐(21)과; 일측이 상기 분출노즐(21)에 설치되어 용존오존수의 공급경로를 제공하는 오존수 공급관로(22)와; 상기 오존수 공급관로(22)의 단부에 설치되며, 오존가스를 여과수에 용해시킨 용존 오존수를 주입하는 용존오존수 주입장치(7)로 구성된다.The wastewater precision filtration apparatus using the metal membrane according to the present invention is implemented to efficiently perform membrane cleaning by injecting dissolved ozone water in which ozone gas is dissolved in filtered water to the metal membrane. As shown, the reaction tank (1) for receiving the raw water (3) introduced from the outside to provide a space for depositing the sludge; It is installed in the inner center of the reaction tank (1), the separation plate (8) for upright and spaced apart by a predetermined distance so that the raw water (3) flows smoothly; A filtration membrane module (2) installed at one side of the separation plate (8), that is, in a space opposite to the direction in which the raw water (3) flows in and allowing the raw water (3) to rise to perform solid-liquid separation; A suction pipe 5 having one end installed on an upper portion of the filtration membrane module 2 and providing a path for sucking and discharging the filtered water 4 passing therethrough; It is installed at a predetermined position of the suction pipe (5), and forcibly sucks out the filtered water (4) passing through the filtration membrane module (2), while maintaining the inside of the filtration membrane module (2) at a negative pressure solids of the filtered water (4) A suction pump 6 for separation being performed; A jet nozzle 21 mounted at a lower part of the filtration membrane module 2 to jet dissolved ozone water upward to perform membrane cleaning of the filtration membrane module 2; An ozone water supply pipe 22 having one side installed in the jet nozzle 21 to provide a supply path of dissolved ozone water; It is provided at the end of the ozone water supply passage 22, and is composed of a dissolved ozone water injector 7 for injecting dissolved ozone water in which ozone gas is dissolved in filtered water.
여기서, 상기 여과막 모듈(2)은 상면에 흡인관(5)과 연결되는 흡인구(11)가 설치되고, 하단부에는 분출노즐(21)과 연결되는 오존수 주입구(12)가 구비되며, 양측면이 개방된 여과 틀체(10)와; 상기 여과 틀체(10)의 양측면에 설치되는 금속막(9)을 포함한다.Here, the filtration membrane module 2 is provided with a suction port 11 is connected to the suction pipe 5 on the upper surface, the lower portion is provided with an ozone water injection port 12 connected to the jet nozzle 21, both sides are open A filtration framework 10; It includes a metal film (9) provided on both sides of the filter frame (10).
특히, 본 실시예에서의 여과막 모듈(2)은 여과를 위해 차지하는 처리시스템의 소요면적을 줄일 수 있는, 즉 같은 반응조(1)내에서 집적밀도를 높이기 위해 평막형의 상자로 이루어진 구조로 되어 있다.In particular, the filtration membrane module 2 in the present embodiment has a structure of a flat membrane box to reduce the required area of the processing system occupying for filtration, that is, to increase the density of integration in the same reaction tank 1. .
또한, 상기 여과막 모듈(2)에서의 금속막(9)은 유효여과면적이 양면합계 0.12m2이고, 막공경은 0.2μm 이다. 특히 상기 금속막(9)은 기존의 막분리시스템에서 주로 사용되어 온 유기성 재질 성분계의 막재질보다 내구성, 내충격성, 내화학약품성이 뛰어난 서스316L(sus316L)의 스테인레스재질로 이루어질 수 있다. 본 실시예에서의 상기 금속막(9)은 SUS316L의 스테인레스강 금망에 스테인레스강 분말을 도포하여 소결한 구조로 되어 있다.In addition, the metal membrane 9 of the filtration membrane module 2 has an effective filtration area of 0.12 m 2 on both sides and a membrane pore diameter of 0.2 μm. In particular, the metal film 9 may be made of stainless steel of sus316L (sus316L) having superior durability, impact resistance, and chemical resistance than the organic material component-based membrane material that is mainly used in the conventional membrane separation system. The metal film 9 in this embodiment has a structure sintered by applying stainless steel powder to a stainless steel gold mesh of SUS316L.
상기 용존오존수 주입장치(7)는 플라즈마에 의해 공기중의 산소를 오존으로 변환시키고, 고압을 이용해 상기 오존가스를 여과수에 용해시키는 플라즈마 장치를 포함하며, 간헐적인 방식으로 용존오존수를 주입하는 구조로 이루어져 있다.The dissolved ozone water injection device 7 includes a plasma device that converts oxygen in the air into ozone by plasma, and dissolves the ozone gas in the filtered water using high pressure, and injects the dissolved ozone water in an intermittent manner. consist of.
상기와 같이 구성된 본 고안의 작용상태를 설명하면 다음과 같다.Referring to the working state of the present invention configured as described above are as follows.
도면에 도시된 바와 같이, 여과막 모듈(2)이 반응조(1)내의 원수에 침적된 상태에서, 상기 반응조(1)의 유입구를 통하여 원수(3)가 유입되면, 원수(3)의 흐름은 분리판(8)에 부딪히면서 하강류를 형성하게 된다. 상기 원수(3)는 하강류에 의해 상기 반응조(1)와 분리판(8) 하부의 사이 공간을 경유하여 U턴함으로써 상승하여 여과막 모듈(2)측으로 유입된다.As shown in the figure, in the state in which the filtration membrane module 2 is deposited on the raw water in the reaction tank 1, when the raw water 3 is introduced through the inlet of the reaction tank 1, the flow of the raw water 3 is separated. It strikes the plate 8 and forms a downflow. The raw water 3 is raised by U-turn through the space between the reaction tank 1 and the lower part of the separator plate 8 by the downward flow, and flows into the filtration membrane module 2 side.
이때, 상기 흡입펌프(6)의 가동에 의해 여과막 모듈(2) 내부 압력을 여과막 모듈 외부의 압력보다 작게한 흡인여과방식을 통해 고액분리를 행한다. 즉, 상기 흡인펌프(6)로부터 제공되는 흡입력에 의해 상기 여과막 모듈(2)을 통과하는 여과수(4)를 강제 흡인하여 흡인관(5)을 통해 배출하며, 또한 상기 흡입력은 상기 여과막 모듈(2)의 내부를 부압으로 유지시키게 되는데, 이때의 상기 부압에 의해 원수의 고액분리가 용이하게 행해지게 되는 것이다. 상기 원수(3)의 고액분리가 행해지고 난 후에 반응조(1) 하부로 침적되는 잉여슬러지는 드레인을 통하여 외부로 배출된다.At this time, the solid-liquid separation is performed through a suction filtration method in which the pressure inside the filtration membrane module 2 is lower than the pressure outside the filtration membrane module by the operation of the suction pump 6. That is, the suction water supplied from the suction pump 6 forcibly sucks the filtered water 4 passing through the filtration membrane module 2 and discharges it through the suction pipe 5, and the suction force is the filtration membrane module 2. The inside of the is maintained at a negative pressure, the solid-liquid separation of raw water is easily performed by the negative pressure at this time. After the solid-liquid separation of the raw water 3 is performed, excess sludge deposited in the lower part of the reaction tank 1 is discharged to the outside through the drain.
상기 여과막 모듈(2)를 통한 원수(3)의 고액분리가 행해지는 과정에서, 상기 용존오존수 주입장치(7)에서 만들어진 용존오존수가 공급관로(22)에 간헐적으로 주입되고, 상기 용존오존수는 분출노즐(21)을 경유하여 상기 여과막 모듈(2)의 상측으로 분사되어 금속막을 세정하게 된다.In the process of solid-liquid separation of the raw water 3 through the filtration membrane module 2, the dissolved ozone water produced by the dissolved ozone water injector 7 is intermittently injected into the supply line 22, and the dissolved ozone water is ejected. It is sprayed to the upper side of the filtration membrane module 2 via the nozzle 21 to clean the metal membrane.
이때, 상기 금속막을 세정할 때, 상기 분출노즐(21)은 용존오존수를 금속막의 여과수(4)측으로부터 유입원수측으로 분출시킴으로써 막투과유속을 현저하게 회복할 수 있다. 특히, 상기 금속막의 여과압력을 60 ∼ 90(kPa)의 범위로 운전하고, 용존오존농도는 0.2 ∼ 0.8(mgO3/L)이상으로 하되, 용존오존농도를 조절할 경우, 초기 막투과 유속의 88 ∼ 97%정도의 회복효과를 나타낼 수 있는데, 시험결과 용존 오존농도가 높을수록 그 회복효과가 보다 월등한 것으로 나타났다.At this time, when cleaning the metal film, the jet nozzle 21 can remarkably recover the membrane permeation flow rate by ejecting the dissolved ozone water from the filtered water 4 side of the metal film to the inflow water side. In particular, when the filtration pressure of the metal film is operated in the range of 60 to 90 (kPa), and the dissolved ozone concentration is 0.2 to 0.8 (mgO 3 / L) or more, but the dissolved ozone concentration is adjusted, the initial membrane permeation flow rate 88 The recovery effect was about 97%. The higher the dissolved ozone concentration, the better the recovery effect.
이와같이, 산화력이 강한 용존오존수를 금속 여과막 모듈(2)의 내외부에 주입하여 내부 파울링 현상 및 막표면에 케익층(Cake layer)이 형성되는 것을 방지함으로써 항시 높은 막투과유속을 유지할 수 있는 것이다Thus, by injecting the oxidizing strong dissolved ozone water into the inside and outside of the metal filtration membrane module 2 to prevent the internal fouling phenomenon and the formation of a cake layer on the membrane surface (Cake layer) can always maintain a high membrane permeation flow rate
다음, 상기 금속막 반응조를 사용한 여과실험에서 세정효과에 대한 결과에 대해서 설명한다. 하기의 <표1>은 세정에 의한 막투과유속의 회복상황을 비교하기 위하여 여과 및 세정실험을 행하였을 때의 각각의 실험조건을 나타낸 것이다.Next, the results of the cleaning effect in the filtration experiment using the metal membrane reaction tank will be described. Table 1 below shows the experimental conditions when the filtration and washing experiments were performed to compare the recovery of the membrane permeation flow rate by washing.
세정방법은 4가지 경우를 대상으로 하는데, 이는 1. 공기에 의한 역세정, 2. 오존가스에 의한 역세정, 3. 용존오존수에 의한 역세정, 4. 화학약품액에 의한 세정등의 방법으로 세정후의 막투과유속의 회복정도를 비교하였다.The cleaning method is applied to four cases, including 1. backwashing with air, 2. backwashing with ozone gas, 3. backwashing with dissolved ozone water, 4. washing with chemical liquid, etc. The degree of recovery of the membrane permeation flux after washing was compared.
하기의 <표1>에서 오존농도(mg/L)는 오존함유가스 1리터당 오존량을 나타내며 주입유량(L/min)은 오존함유가스의 공급유량을 의미한다. 공기, 오존가스 및 용존오존수에 의한 세정에서는 세가지의 경우 모두 여과주기를 10분 여과, 1분정지, 세정주기를 2분역세, 2분정지로 실험조작을 행하게 되는데, 이때의 1사이클은 15분이 된다. 즉, 본 발명에 있어서 1 사이클의 의미는 여과조작과 세정조작을 각각 1회 조합한 것으로 한다.In Table 1 below, the ozone concentration (mg / L) represents the amount of ozone per liter of the ozone-containing gas and the injection flow rate (L / min) means the supply flow rate of the ozone-containing gas. In the case of cleaning by air, ozone gas and dissolved ozone water, all three experiments are performed by filtration cycle for 10 minutes, 1 minute stop, washing cycle for 2 minutes, and 2 minutes for one cycle. do. That is, in the present invention, one cycle means combining the filtration operation and the washing operation once.
약품세정의 경우, 여과주기는 다른 세정방법과 동일하게 실시하였으나 세정의 경우 NaOCl의 농도 100mg/L의 용액에 20분간 침적시키는 것으로 세정을 행하였다. 오존농도에서 가스상태의 농도 30mgO3/L는 오존가스로 역세정을 한 경우의 오존발생농도에 해당되며 용존상태의 0.2 ∼ 0.8 mgO3/L는 용존오존수로 역세정을 행한 경우의 용존오존농도를 의미한다. 각각의 경우에 대해 120시간동안 세정효과를 실험적으로 검토하였다.In the case of chemical cleaning, the filtration cycle was carried out in the same manner as in the other washing methods, but in the case of washing, washing was performed by dipping for 20 minutes in a solution having a concentration of 100 mg / L NaOCl. Concentration 30mgO gaseous ozone concentration 3 / L was dissolved ozone concentration in the case, and the ozone generation concentration in the case where the back washing with the ozone gas subjected to reverse washing with 0.2 ~ 0.8 mgO 3 / L was dissolved ozone water dissolved state Means. For each case, the cleaning effect was experimentally examined for 120 hours.
도3은 상기 <표1>에 나타낸 조작인자에 따른 세정을 실시하였을 경우의 막투과유속의 비(Javerage/Jinitial)를 나타낸 것이다. 즉, 막투과유속의 비(Javerage/Jinitial)는 120시간동안의 평균 막투과유속을 초기 1분간의 막투과유속으로 나눈 값을 의미한다.Fig. 3 shows the ratio ( Javerage / Jinitial ) of the membrane permeation flow rate when the cleaning is performed according to the operating factors shown in Table 1 above. That is, the ratio of membrane permeation flux ( Javerage / Jinitial ) means a value obtained by dividing the average membrane permeation flux for 120 hours by the membrane permeation flux for the first minute.
도3에 나타난 결과에서 알 수 있듯이, 용존오존수를 이용한 세정효과는 약품세정을 이용한 방법 및 단순한 공기를 이용한 방법보다 우수한 세정효과를 보였다. 용존오존농도가 0.7 mgO3/L 인 경우 오존수를 이용하여 역세정을 한 경우, 초기 막투과유속의 97%의 회복율을 보였으며, 용존오존농도가 0.2 mgO3/L인 경우에도 초기 막투과유속의 88% 의 회복율을 나타내었다. 반면 공기를 이용한 세정방법과 화학약품을 이용한 세정방법의 경우에는 각각 62% 와 68%의 회복률을 보여 70%에도 미치지 못하는 세정효과를 나타냈다. 오존가스를 이용하여 막세정을 행한 경우 막투과 유속의 비가 0.91로 비교적 높은 회복률을 보였지만, 여과를 행할 경우 막모듈 내부에 잔존하는 오존가스를 제거해야 하는 운전관리상의 어려움이 있을 것으로 사료된다.As can be seen from the results shown in Figure 3, the cleaning effect using the dissolved ozone water showed a superior cleaning effect than the method using the chemical cleaning and the method using a simple air. In case of dissolved ozone concentration of 0.7 mgO 3 / L, backwashing with ozone water showed 97% recovery of initial membrane permeation flow rate, and initial membrane permeation flow rate even at dissolved ozone concentration of 0.2 mgO 3 / L Recovery rate of 88% was shown. On the other hand, the air cleaning method and the chemical cleaning method showed 62% and 68% recovery rate, which was less than 70%. Membrane cleaning using ozone gas showed a relatively high recovery rate (0.91) of the membrane permeation flow rate, but it is considered that there is a difficulty in operation management to remove the ozone gas remaining inside the membrane module.
결과적으로 용존오존수를 이용한 세정방법은 막오염을 효과적으로 제거함을 알 수 있었고, 용존오존 농도가 증가할수록 세정효과가 증가하는 것으로 나타났다.As a result, it was found that the cleaning method using dissolved ozone water effectively removed the membrane contamination, and the cleaning effect increased as the dissolved ozone concentration increased.
본 실험이 종료된 시점에서 금속막의 외관을 관찰한 결과 일반적으로 유기재질의 막에서는 흔히 관찰되는 막재질의 산화파손현상은 전혀 나타나지 않아 사용된 금속막은 오존에 대해 충분한 내성을 지니는 것으로 판명되었다.As a result of observing the appearance of the metal film at the end of the experiment, it was found that the oxidative damage phenomenon of the film material, which is commonly observed in the organic film, was not found at all, and thus the metal film used was sufficiently resistant to ozone.
이상에서 설명한 본 발명은 전술한 실시예 및 첨부된 도면에 의해 한정되는 것이 아니고, 본 발명의 기술적 사상을 벗어나지 않는 범위 내에서 여러 가지 치환, 변형 및 변경이 가능하다는 것이 본 발명이 속하는 기술분야에서 통상의 지식을 가진 자에게 있어 명백할 것이다.The present invention described above is not limited to the above-described embodiments and the accompanying drawings, and various substitutions, modifications, and changes are possible in the art without departing from the technical spirit of the present invention. It will be clear to those of ordinary knowledge.
전술한 바와 같이 본 발명에 따르면, 막분리시스템의 적용에 있어서, 용존 오존수에 대한 내구성이 강한 금속막을 채용하되, 용존오존수를 이용한 간헐적 세정방식을 행함으로써 내부 파울링 현상을 방지하고 공기방울의 발생을 억제하여 여과막 표면적의 사공간(dead space)을 제거함으로써 막투과 유속의 회복율을 제고시킬 수 있으며, 기존의 물리 ·화학적방법들이 지니고 있던 막세정의 번잡성을 해결하여 시스템 운용의 효율성을 극대화할 수 있는 효과를 가진다.As described above, according to the present invention, in the application of the membrane separation system, a metal film having a high durability against dissolved ozone water is employed, but intermittent cleaning method using dissolved ozone water prevents internal fouling and generates air bubbles. It is possible to improve the recovery rate of membrane permeation flow rate by removing dead space of filtration membrane surface area, and to maximize the efficiency of system operation by solving the complexity of membrane cleaning existing physical and chemical methods. Has the effect.
또한, 본 발명은 오존에 대한 내구성에 강하며, 비교적 저렴한 금속막을 사용하여 오·폐수의 고액분리를 달성할 수 있는 다른 효과가 있다.In addition, the present invention is resistant to ozone, and has another effect of achieving solid-liquid separation of wastewater by using a relatively inexpensive metal film.
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| KR101270647B1 (en) * | 2010-01-27 | 2013-06-03 | 한국기계연구원 | Membrane filter system having function for preventing fouling |
| KR20190034853A (en) | 2017-09-25 | 2019-04-03 | (주)미시간기술 | generating equipment of disolved-ozonic water and the generating method using thereof |
| CN117232690A (en) * | 2023-11-14 | 2023-12-15 | 山东辰智电子科技有限公司 | Ultrasonic heat meter |
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| KR101270647B1 (en) * | 2010-01-27 | 2013-06-03 | 한국기계연구원 | Membrane filter system having function for preventing fouling |
| KR20190034853A (en) | 2017-09-25 | 2019-04-03 | (주)미시간기술 | generating equipment of disolved-ozonic water and the generating method using thereof |
| CN117232690A (en) * | 2023-11-14 | 2023-12-15 | 山东辰智电子科技有限公司 | Ultrasonic heat meter |
| CN117232690B (en) * | 2023-11-14 | 2024-02-09 | 山东辰智电子科技有限公司 | Ultrasonic heat meter |
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