KR101239249B1 - Sewage and waste water advanced treatment system for energy saving - Google Patents

Abstract

PURPOSE: A sewage/wastewater advanced processing system is provided to minimize the blockage of a separation film for the continuous operation, to prevent the generation of a pin floc, and to maximize the operation efficiency by improving the cleansing cycle using a reverse cleansing cycle drug. CONSTITUTION: A sewage/wastewater advanced processing system for saving energy includes a reaction tank(100) for the biological water treatment reaction, a separation film tank(200), a sludge returning line, a suction facility(600), and a blower(700). The separation film tank is divided into an aeration area and a non-aeration area, and includes a separation film module(221) with a separation film which is installed on the non-aeration area for filtering processing water. Plural inclined plates are installed on the bottom of the separation film module for preventing the blockage of the separation film. A solid-liquid separator(222) which flows the processing water from the lower side to the upper side is installed among the inclined plates.

Description

Energy-Saving Wastewater Advanced Treatment System {SEWAGE AND WASTE WATER ADVANCED TREATMENT SYSTEM FOR ENERGY SAVING}

The present invention relates to an advanced sewage treatment system using a separation membrane, and more particularly, to an advanced energy saving sewage treatment system in which sewage or wastewater treated in a reaction tank is filtered through a separation membrane and separated into final treated water.

The advanced treatment of sewage or wastewater is largely divided into Continuous-F Low Process (SBR) and Sedimentation Batch (SBR) which allocates sedimentation time in the reactor without separate sedimentation tank.

The continuous flow method is to set up each reaction tank, that is, anaerobic, anoxic tank, aerobic tank and sedimentation tank separately to make the conditions of anaerobic, anoxic, aerobic and sedimentation required for wastewater treatment, mainly used in medium and large sewage treatment plants In case of heavy flow rate or fluctuations in water quality, the capacity to cope is poor. Typical processes include A / O (Anaerobic and Oxidation), A2 / O (Anaerobic-Anoxic-Oxic), DNR (Daewoo Nutrient Removal) and Bardenpho method.

In addition, the continuous batch method is composed of a single reaction tank that does not require a precipitation tank, and the process is divided into an inflow step, a reaction step, a precipitation step and a discharge step by giving conditions of anaerobic, anoxic, aerobic and precipitation in a single reaction tank. It is mainly used in small and medium sized sewage treatment plants, and has the advantage of being able to cope with an increase in flow rate and water quality fluctuation.

The World Environmental Association (WEF) also has a continuous batch method that can be easily applied in small cities with few sites, and has excellent applicability according to the characteristics of sewage and wastewater. It is considered very suitable on a very small scale. In addition, continuous batch methods include Kuho & KIST Intermittently Decanted Extended Aeration (KIDEA), Intermittent Decanted Extended Aeration (IDEA), and swirling vortex type SBR.

In addition, two to four reactors are divided into anaerobic, anaerobic, and aerobic states as structures such as A / O, A2 / O, and Bardenpho. The development of advanced treatment process has been developed by the operation of the reaction tank that changes the operation of the reactor over time, and in particular, a flow change activated sludge or an intermittent aeration type treatment method which is effective in treating nitrogen is developed and used. A major focus of these methods is the effective use of organics in the anaerobic or anaerobic phase, which is the stage of denitrification and phosphorus release.

Recently, many technologies have been developed by incorporating a separation membrane into an existing high processing method. Most of the technologies related to the separation membrane process were developed by immersing the separation membrane in the reactor, and the microorganisms in the reactor can be maintained at a high concentration, so that a high treatment efficiency can be obtained at a short residence time (HRT), and the physical solid solution separation is performed. The treatment water quality is very stable, and it is possible to maintain high concentration of activated sludge in the aeration tank during high concentration sewage and wastewater treatment, as well as to accumulate high nitrification microorganisms with sludge age (SRT). There is an advantage that can be reduced is widely used now.

For example, the treatment method using the separation membrane shown in FIG. 1 performs denitrification in the anaerobic tank 1, release of phosphorus in the anaerobic tank 2, nitrification and intake of phosphorus in the aerobic tank 3, and water treatment using the separation membrane 4, Sludge adheres to the separation membrane 4, and a gel layer is formed due to the adhered sludge, so that a phenomenon in which the filtration rate is reduced and the water treatment capacity is lowered occurs. As such, when the membrane 4 is contaminated, the internal pressure is increased due to the polarization of concentration, the permeate amount is reduced, and the replacement cycle of the membrane is shortened, thereby reducing the lifespan.

In addition, there is a limit in maintaining a high flux due to contamination of the separator 4, and the main cause for this is to promote fouling of the membrane by maintaining a high concentration of microorganisms in the reactor, Permanent blockage of the separator is accelerated by the floc).

As such, clogging of the separator 4 occurs frequently, and only a short operation period (for example, start: stop = 0.7: 0.3) of the separator 4 may limit the operation time and operation efficiency of the separator.

Therefore, when the membrane is contaminated, the membrane contamination prevention chemical is added, or after use, the membrane 4 contaminated with caustic soda, trisodium, citric acid, sodium hypochlorite, phosphoric acid and hydrochloric acid is washed. Due to the strong toxicity to microorganisms, the treatment efficiency becomes unstable at the initial stage after washing, and there is a problem that economical loss occurs because treatment and management of washing water is required.

In addition, as shown in FIG. 1, a method of washing the separation membrane 4 in an over-aeration manner by injecting excessive air generated from the air injector 5 of the aerobic tank 3 has also been developed, but with only physical force using air bubbles. There is a limit to the removal of the gel layer attached to the separator 4, and excessive air injection for cleaning the separator 4 not only makes it difficult to maintain the proper air in the aeration tank 3, but also due to the aeration causes dissolved oxygen. A separate process called an abatement tank is added and there is a problem of excessive consumption of energy.

In addition, a method of injecting a flocculant into the reaction vessel has also been proposed, but the filtration resistivity of natural particles is about 1.7 times greater than that of artificial particles produced by flocculant injection. In case of over-injection of coagulant, it is toxic to nitrifying and denitrifying microorganisms, and the growth rate of microorganisms is slow. Especially, nitrifying microorganisms sensitive to external environmental conditions are caused by metal salts due to coagulant injection. It acts as a limiting factor of microbial growth, there is a problem that the concentration of the metal salt acts as a limiting factor in the removal of organic matter of the microorganism.

In addition, the conventional sewage treatment process using the membrane is a system that requires the sludge conveyance, the sludge conveyance to maintain the active microorganism in the reaction tank and maintains a high sludge conveyance rate to improve the denitrification performance, which is a sewage treatment process It can have a fatal adverse effect on it. Especially, it contains a large amount of NOx and high DO concentration in the return water, which acts as a major cause of suppressing P-release. There is a problem of consumption.

The present invention has been made to solve all the above-described problems, it is possible to reduce the concentration of MLSS in the separation membrane tank, prevent the formation of pin flocs, minimize the fouling of the membrane (continuous operation), It is possible to maximize the operating efficiency by greatly improving the cleaning cycle for preventing contamination of the membrane, and to zero the energy consumed for supplying the enormous amount of air that was conventionally used for preventing the contamination of the membrane. It can be operated in the same way, there is no need to install additional facilities, can actively cope with low carbon and green growth, and can operate the sludge conveyance rate low, which can save energy and reduce the sludge load of the membrane module. Its purpose is to provide an advanced wastewater treatment system.

In addition, due to the characteristics of domestic sewage, it prevents the deterioration of the total nitrogen (TN) and total phosphorus (TP) treatment due to the low C / N ratio, and provides an advanced sewage treatment system that can efficiently supply and operate the organic carbon source among influent raw water. Has a purpose.

In order to solve the above problems, the energy-saving wastewater advanced treatment system of the present invention includes a reaction tank 100 in which a biological water treatment reaction is performed; The treated water treated in the reaction tank 100 is separated into final treated water, and an aeration pipe 210 is installed and an aeration area 210 in which air is supplied and a non-aeration area 220 which are not supplied are partition walls. The separation membrane tank 200 in which the separation membrane module 221 is formed so as to be separated by the 230, and the separation membrane 221a is formed in the non-aeration region 220 to filter the introduced treated water into the final treated water. ); A sludge conveying line 400 for conveying the sludge deposited in the separation membrane tank 200 to the reaction tank 100 using a sludge conveying pump 410; A suction device 600 connected to the membrane separation module 221 so that a pressure difference necessary for membrane separation in the separation membrane tank 200 is formed; And a blower 700 for supplying air to the aeration region 210 of the separation membrane tank 200 to blow air through the connected diffuser 211. The separation membrane module 221 A plurality of inclined plates 222a are provided at a lower side of the separator to prevent clogging of the separation membrane 221a, and a solid-liquid separation is provided between the inclined plate 222a and the inclined plate 222a with a flow path through which the treated water moves from the lower side to the upper side. A facility 222 is installed, and irradiates ultrasonic waves toward the separation membrane 221a next to the separation membrane module 221 to clean the separation membrane 221a, and an ultrasonic irradiation plate 223a and the ultrasonic irradiation plate ( An ultrasonic irradiator 223 coupled to 223a and including an ultrasonic irradiator 223b for irradiating ultrasonic waves toward the separator 221a is installed, and the ultrasonic irradiator 223b has a strong cavitation strength of 20 kHz to 500 kHz. With the frequency of the band Ultrasonic waves, penetration is strong, ultra-high frequency of 1.0MHz or more capable of ultra-fine cleaning in parallel to irradiate multiple waves, the inclined plate (222a) is formed to be inclined at an angle of 50 ° to 70 ° relative to the horizontal plane, preventing the injuries of sludge The upper and lower blocking baffles 222b and 222c are respectively formed on the upper and lower sides thereof, and the whole is coated with a micro hydrophobic material. The micro hydrophobic materials include TiO2, SnO2, ZnO, WO3, Nb2O5, TiSrO3, It is characterized in that the metal oxide fine particles selected from the group consisting of Anatase-type TiO2.

Here, the treated water of the aeration region 210 may be configured to overflow through the top of the partition 230 to flow into the non-aeration region 220.

In addition, the non-aeration area 220 is provided with a vertical plate 224 in a vertical direction while being spaced apart from the partition wall 230, and the treated water introduced from the aeration area 210 may be separated from the partition wall 230. It may be configured to flow downward through the inflow path 225 formed between the direct plate 224.

In addition, the bottom surface of the non-aeration region 220 may be formed to be inclined downward from the partition wall 230, and may be configured to collect and concentrate sludge in the sludge collection hopper 226 formed at the distal end of the bottom surface. .

A pin floc discharge pipe 900 for discharging the pin floc included in the supernatant to the outside may be installed at one side of the membrane module 221.

The reactor 100 may be installed such that a pair of first and second alternating reactors 100a and 100b are arranged in parallel to communicate with each other by the outlet sleeve 110.

Further, the first and second outflow equipments 310 and 320 are respectively provided with first and second outlet valves for allowing the treated water treated in the first and second alternating reaction tanks 100a and 100b to flow into the separation tank 200. It can be configured to include.

The suction device 600 is connected to the separator module 221 and is installed on the suction pipe 610 and the suction pipe 610 for sucking and discharging the final treated water separated by the separator 221a to the outside. It may include a suction pump 620 for adjusting the suction pressure.

It may further include a hydrocyclone 500 is installed on the sludge conveying line 400 and the solid-liquid separation of the sludge and the filtrate therein by the pressure of the sludge conveying pump 410.

According to the present invention, by installing a solid-liquid separator at the bottom of the membrane module to reduce the concentration of MLSS inside the membrane tank, to prevent the formation of pin flocs, to minimize the clogging (fouling) of the membrane as well as continuous operation is possible In order to maximize the operation efficiency by greatly improving the cleaning cycle by the reverse cleaning cycle chemicals to prevent the contamination of the membrane, the energy consumed for supplying the enormous amount of air that was conventionally used to prevent the contamination of the membrane It can be zero and can be operated economically and stably, there is no need to install additional facilities, and it can effectively cope with low carbon and green growth.

In addition, the inclined plate is installed at an angle of 50 ° to 70 ° to prevent blockage of the membrane under the separator module installed in the non-aeration area, and the entire inclined plate is TiO2, SnO2, ZnO, WO3, Nb2O5, TiSrO3, and anatase-type. Coated with a very hydrophobic material selected from the group consisting of TiO2 of the), thereby forming a fine air layer between the wastewater or sewage and the slant plate, thereby preventing the microorganisms contained in the wastewater or the sewage from sticking to the slant plate and carrying the sludge Hydrocyclone is installed in the line, and the high-pressure rotational power using the high pressure of the pump separates the solids into high concentration sludge and filtrate, which increases the concentration of the return sludge, which can operate the sludge conveyance rate low, and saves energy.The sludge of the membrane module It also has the effect of reducing the load.

In addition, it is possible to prevent the performance degradation of total nitrogen (TN) and total phosphorus (TP) treatment due to the low C / N ratio, and to provide an advanced sewage treatment system that can efficiently supply and operate organic carbon sources among influent raw water. It also works.

1 is a view of a water treatment apparatus having a conventional separator.
Figure 2 is a schematic diagram showing the configuration of the advanced energy-saving sewage treatment system.
Figure 3 is a plan view showing the configuration of the energy-saving wastewater advanced treatment system according to the present invention.
Figure 4 is a schematic diagram showing the configuration of the separation membrane tank of the energy-saving wastewater advanced treatment system according to the present invention.

The inventors of the present invention have a water treatment apparatus using a conventional separation membrane, sludge is attached to the membrane is contaminated, the gel layer is formed due to the attached sludge, the clogging is continued by the pin floc, the water treatment capacity is reduced, the replacement cycle is shortened life In addition, when chemicals or flocculants are added to prevent membrane contamination, the microorganisms are toxic to microorganisms, resulting in unstable and uneconomical treatment efficiency, and it is difficult to maintain proper air due to overaeration when the membrane is washed in an over-aeration manner. It has been recognized that there is a problem that excessive energy is consumed, and that a high sludge conveyance rate is maintained to reduce treatment efficiency and excessive energy is consumed.

Accordingly, the present inventors have made a lot of research and efforts to solve the above problems, install a solid-liquid separator at the bottom of the membrane module to reduce the concentration of MLSS in the membrane tank, prevent the formation of pin floc, In addition to minimizing fouling, continuous operation is not only possible, but also greatly improves the cleaning cycle by reverse cleaning cycle chemicals to prevent contamination of the membrane. The energy consumed for the enormous amount of air supplied can be zeroed, so it can be operated economically and stably, there is no need to install additional facilities, actively cope with low carbon and green growth, and also in the sludge conveying line. High concentration sludge and filtration through high-speed rotational power using high pressure of pump by installing hydrocyclone It can reduce the sludge conveyance rate by increasing the concentration of conveying sludge by solid-liquid separation, and it can save energy, reduce sludge load of membrane module, and total nitrogen (TN) due to low C / N ratio in domestic sewage characteristics. The present invention relates to an advanced energy-saving sewage treatment system capable of preventing deterioration of the total phosphorus (TP) and total phosphorus (TP) treatment and efficiently supplying and operating organic carbon sources in the influent raw water.

Hereinafter, the configuration of the present invention will be described in detail with reference to the drawings with reference to the drawings.

Energy saving type sewage treatment system according to an embodiment of the present invention, as shown in Figures 2 and 3, the reaction tank 100 is a biological water treatment reaction is performed, and the treated water treated in the reaction tank 100 Water treatment system comprising a separation membrane tank 200 is separated into the final treated water, in addition to the first and second outflow equipment (310,320), sludge conveying line 400, hydrocyclone (500), suction equipment 600 ), A blower 700, the electric control panel 800 and the pin floc discharge pipe 900 may be further provided.

The reaction tank 100 may be reacted with water, but a pair of first and second alternating reaction tanks 100a and 100b may be disposed in parallel to communicate with each other by the outlet sleeve 110.

When the raw water introduced from the inlet facility (not shown) is described in detail by the reaction tank 100, step a), by changing the flow path of the inlet facility, raw water is alternately supplied according to the distribution of a predetermined time. , 70 to 90% of the raw water is introduced into the first shift reactor (100a), the remaining 10 to 30% of the raw water is introduced into the second shift reactor (100b), the first shift reactor ( The raw water introduced into 100a is discharged into the second alternating reaction tank 100b through the outlet sleeve 110, and then a second outlet valve is opened to open the separation membrane tank 200 through the second outlet facility 320. In this case, air is selectively supplied from the blower 700 only to the separation membrane tank 200.

In step b), after 100% of the raw water flows from the inflow equipment to the first shift reactor 100a, the first outlet valve is opened and flows out to the separation membrane tank 200 through the first outlet equipment 310. The second shift reactor 100b forms anaerobic conditions while the inflow of raw water is short-circuited to maximize the release of phosphorus. At this time, air is selectively supplied from the blower 700 only to the separation tank 200.

In step c), the raw water is alternately supplied according to the distribution of the predetermined time by changing the flow path of the inflow equipment, and 70 to 90% of the raw water is introduced into the second shift reactor 100b from the inflow equipment, and the rest of the raw water Phosphorus 10 to 30% is introduced into the first shift reactor (100a), the raw water introduced into the second shift reactor (100b) is discharged to the first shift reactor (100a) through the outlet sleeve (110). Afterwards, the first outlet valve is opened and flows out to the separation tank 200 through the first outflow facility 310, where air is selectively supplied from the blower 700 only to the separation tank 200.

In step d), after 100% of the raw water flows from the inflow equipment to the second shift reactor 100b, the second outlet valve is opened and flows out to the separation membrane tank 200 through the second outlet equipment 320. The first alternate reaction tank 100a forms anaerobic conditions while the inflow of raw water is short-circuited to maximize the release of phosphorus. At this time, air is selectively supplied from the blower 700 only to the separation tank 200.

Here, the steps a) and c) are the same operating time, the steps b) and d) are the same operating time, the ratio of the operating time of steps a) and b) is 1: 0.5 to 1 It is preferable to operate at a ratio of 2: 2.

And, step b) and step d) can be more effective when the load of the incoming raw water is extremely low, and step b) and d) can be operated variably when more than the planned load. .

As shown in FIG. 4, the separation membrane tank 200 includes an aeration region 210 in which an diffuser 211 is installed to supply air introduced from the blower 700, and a non-aeration region 220 that is not. It is formed to be separated by the partition wall 230.

In this case, the aeration region 210 is preferably operated in the range of 1.0 ~ 2.5 mg / L dissolved oxygen concentration through the air supply from the blower 700 to the diffuser (211).

In addition, it is preferable that one side of the membrane module 221 is provided with a pin floc discharge pipe 900 for discharging the pin floc included in the filtered supernatant to the outside.

The non-aeration zone 220 is not supplied with air as the aeration zone 210, but is divided into an aerobic tank because dissolved oxygen is included in the treated water introduced, and the non-aeration zone 220 is Inhibition of denitrification can be prevented due to the high concentration of dissolved oxygen during sludge conveyance by inducing consumption.

Here, the sludge residence time (HRT) of the non-aeration region 220 is preferably determined through an OUT-TEST (Oxidation Uptake Rate Test), the range of 5 to 30 minutes is appropriate, if the residence time of more than 30 minutes If provided, endogenous denitrification proceeds and may act as a cause of bulking of sludge.

In addition, the high concentration of MLSS (Mixed Liquor Suspended Solid) in the reactor in the advanced sewage treatment process of the present invention causes membrane contamination, and due to the long sludge residence time, pin flocs are generated, causing permanent membrane blockage. The concentration of the microorganism is preferably 3,000 to 8,000 mg / L.

The membrane tank 200 has a membrane module 221 is installed on the upper portion of the non-aeration area 220, the treated water flows in the reaction tank 100 is filtered by a plurality of membranes (221a), the lower side As such, particulate matter such as sludge in water is precipitated, additional organic matter removal reactions, nitrification and dephosphorization reactions occur, and the final treated water is separated.

In addition, a solid-liquid separation facility 222 is separately installed at the lower side of the separation membrane module 221 to prevent the separation membrane 221a from being blocked.

The solid-liquid separation facility 222 is provided with a plurality of inclined plate (222a) formed to be inclined at a predetermined angle, is introduced from the reaction vessel 100 is blocked by the vertical plate 224 and moved downward through the inflow path 225 The treated water is moved from the lower side to the upper side through the flow path formed between the inclined plate 222a and the inclined plate 222a, and the flow is hindered by the inclined plate 222a installed at the acute angle described above. The sludge is separated and precipitated downward along the inclined plate 222a.

Here, the inclined plate 222a is preferably formed to be inclined at an angle of 50 ° to 70 ° with respect to the horizontal plane, and when the inclination angle is smaller than 50 °, the inclination angle is gentle, so that the sludge settling distance is long and the precipitation efficiency is lowered. When the inclination angle is greater than 70 °, the flow of the treated water moving from the lower side to the upper side is not disturbed, so that the treated water and the mixed mixed water are not separated well.

In addition, the inclined plate 222a has upper and lower blocking baffles 222b and 222c formed in a horizontal direction, respectively, to prevent sludge from rising. That is, the pin floc included in the treated water is floated to contaminate the separation membrane 221a of the separation membrane module 221 installed on the separation membrane tank 200, thereby causing blockage, thereby blocking the membrane in advance and blocking the separation membrane 221a. To minimize this.

In addition, the inclined plate 222a is coated with a very small hydrophobic material, which is to prevent sludge from adhering to or deposited on the inclined plate 222a to form a sludge layer (Slime) to prevent the flow of treated water. to be. That is, the entire sloping plate is coated with one micro hydrophobic material selected from the group consisting of TiO 2, SnO 2, ZnO, WO 3, Nb 2 O 5, TiSrO 3, and Anatase-type TiO 2, thereby providing a fine air layer between the wastewater or sewage and the sloping plate. By forming the microorganisms contained in the wastewater or sewage can not stick to the inclined plate, it does not form a sludge layer.

An ultrasonic irradiation unit 223 may be installed beside the separator module 221 to irradiate ultrasonic waves toward the separator 221a to clean the separator 221a.

In this case, the ultrasonic irradiation unit 223 is coupled to the ultrasonic irradiation plate 223a and the ultrasonic irradiation plate 223a which are installed next to the separation membrane module 221, and irradiates ultrasonic waves toward the separation membrane 221a. 223b may be included.

The ultrasonic irradiation unit 223 periodically applies an ultrasonic shock to the sludge attached to the separator 221a to remove and remove the sludge attached to the separator 221a to maintain the membrane separation performance of the separator 221a to maintain the separation membrane ( Extend the replacement cycle of 221a).

The ultrasonic irradiator 223b is a multi-wave irradiator for generating different ultrasonic waves. The ultrasonic irradiator 223b may be equipped with ultrasonic elements having different structures to generate various frequencies of various bands, and thus high cleaning efficiency may be expected. At this time, the ultrasonic frequency is irradiated in the 20kHz to 500kHz band with strong cavitation strength, and the multi-wavelength irradiation is performed at the ultra-high frequency of 1.0MHz or higher, which has a strong penetration and enables ultra-precision cleaning.

In particular, the cleaning by ultrasonic is strong washing power can be washed most of the separator 221a without a separate washing water, this is because the washing cycle is longer, the use of the washing water is reduced, the secondary effect such as adverse effects on the microorganisms due to the washing water Contamination can be prevented.

In addition, unlike the conventional backwashing method, ultrasonic cleaning is possible even during normal operation of the water treatment device, thereby increasing operating efficiency of the water treatment device.

In addition, the treated water of the aeration region 210 is overflowed through the upper end of the partition wall 230, which is formed somewhat lower than the wall of the separation tank 200 flows into the non-aeration region 220.

Here, the non-aeration area 220 is provided with a vertical plate 224 in the vertical direction in a state spaced apart from the partition 230, the number of the partition wall 230 corresponding to one side of the vertical plate 224 An inflow path 225 is formed between the direct plates 224, and the separation membrane module 221 and the solid-liquid separation facility 222 are installed on the other side of the vertical plate 224.

As a result, the treated water introduced from the aeration region 210 moves toward the bottom surface through the inflow passage 225, and then is solid-liquid separated through the solid-liquid separator 222 while moving from the lower side to the upper side again. Next, the final treated water is separated by filtration by the membrane module 221.

The bottom surface of the non-aeration area 220 is formed to be inclined downward from the partition wall 230 to prevent sludge deposition, and the sludge collecting hopper 226 collecting and collecting sludge on the bottom surface opposite to the partition wall 230. ) Is formed to induce natural collection and concentration of sludge.

The suction facility 600 is connected to the membrane separation module 221 so that a pressure difference necessary for membrane separation in the separation membrane tank 200 is formed, and the suction facility 600 is connected to the separation membrane module 221. And a suction pipe 610 for sucking and discharging the final treated water separated by the separation membrane 221a to the outside, and a suction pump 620 installed on the suction pipe 610 to adjust suction pressure.

In the energy-saving sewage treatment system according to the present invention, the suction pump 620 adjusts the suction pressure by the invert control for continuous operation, and the suction pressure is preferably in the range of -10 to 60 cmHg, wherein the entire system When operating at a minimum suction pressure through the electric control panel 800 to control the operation of each part of the ultrasonic irradiation unit 223 is operated to control the clogging phenomenon of the membrane, not the intermittent operation concept that was the conventional operation method The continuous operation method through the invert control of the suction pump 620 is possible.

The sludge conveying line 400 for conveying the sludge deposited in the separation membrane tank 200 to the reaction tank 100 using a sludge conveying pump 410 is further provided, the hydrocyclone in the sludge conveying line 400 By installing a 500, the solid-liquid separation of high concentration sludge and filtrate through high-speed rotational power using the high pressure of the pump increases the concentration of the conveying sludge, it is possible to operate the sludge conveyance rate is low, the energy saving effect, the membrane module (221) Sludge load can be reduced.

 On the other hand, the energy-saving sewage wastewater treatment system according to the present invention does not require additional facilities such as dissolved oxygen reduction tanks or chemical cleaning tanks required by the conventional membrane water treatment device, thereby reducing installation and operating costs.

As a result, the advanced energy-saving wastewater treatment system according to the present invention installs a solid-liquid separator at the bottom of the membrane module to reduce the concentration of MLSS in the membrane tank, prevent the formation of pin flocs, and fouling of the membrane. Not only enables continuous operation, but also greatly improves the cleaning cycle by the reverse cleaning cycle chemicals to prevent the contamination of the membrane, and maximizes the efficiency of operation. The energy consumed for air supply can be zeroed, so it can be operated economically and stably, there is no need to install additional facilities, proactively cope with low carbon and green growth, and hydrocyclones in the sludge conveying line. Solid-liquid separation into high concentration sludge and filtrate through high-speed rotational power using high pressure of pump As the concentration of return sludge is increased, the sludge conveyance rate can be lowered, which saves energy and reduces the sludge load of the membrane module.In addition, the total nitrogen (TN) and total phosphorus due to the low C / N ratio in domestic sewage characteristics It is possible to prevent deterioration of the (TP) treatment and to operate by efficiently supplying the organic carbon source in the influent.

The present invention is not limited to the above-described embodiments. Anything having substantially the same constitution as the technical idea described in the claims of the present invention and achieving the same operational effect is included in the technical scope of the present invention.

100. Reactor 100a. 1st shift reactor
100b. Second shift reactor 110. Spill sleeve
120. Stirrer 200. Membrane bath
210. Aeration Area 211.
220. Non-aeration zone 221. Membrane module
221a. Separator 222. Solid-liquid Separation Facility
222a. Inclined plate 222b. Top blocking baffle
222c. Lower blocking baffle 223. Ultrasonic irradiation part
223a. Ultrasound irradiation plate 223b. Ultrasonic Irradiator
224. Vertical plates 225. Funnels
226. Sludge collection hopper 230. Bulkhead
310. First outflow facility 320. Second outflow facility
400. Sludge Transfer Line 410. Sludge Transfer Pump
500. Hydrocyclone 600. Suction equipment
610. Suction line 620. Suction pump
700. Blower 800. Electric control panel
900. Pin Flock Discharge Tube

Claims (9)

Reactor 100 in which the biological water treatment reaction is made;
The treated water treated in the reaction tank 100 is separated into final treated water, and an aeration pipe 210 is installed and an aeration area 210 in which air is supplied and a non-aeration area 220 which are not supplied are partition walls. The separation membrane tank 200 in which the separation membrane module 221 is formed so as to be separated by the 230, and the separation membrane 221a is formed in the non-aeration region 220 to filter the introduced treated water into the final treated water. );
A sludge conveying line 400 for conveying the sludge deposited in the separation membrane tank 200 to the reaction tank 100 using a sludge conveying pump 410;
A suction device 600 connected to the membrane separation module 221 so that a pressure difference necessary for membrane separation in the separation membrane tank 200 is formed; And
And a blower (700) for supplying air to the aeration area (210) of the separation membrane tank (200) to eject air through the diffuser (211) connected thereto.
A plurality of inclined plates 222a are provided below the separator module 221 to prevent the separation membrane 221a from being blocked, and the treated water moves from the lower side to the upper side between the inclined plate 222a and the inclined plate 222a. Solid-liquid separation equipment 222 is formed is a flow path is formed,
The ultrasonic membrane is irradiated toward the separation membrane 221a toward the side of the separation membrane module 221 to clean the separation membrane 221a, and is coupled to an ultrasonic irradiation plate 223a and the ultrasonic irradiation plate 223a to form the separation membrane ( An ultrasonic irradiator 223 including an ultrasonic irradiator 223b irradiating ultrasonic waves toward the 221a is installed.
The ultrasonic irradiator 223b irradiates multiple waves in parallel with an ultrasonic wave having a frequency of 20 kHz to 500 kHz with a strong cavitation strength, in parallel with ultra-high frequency of 1.0 MHz or more, which is capable of ultra-precise cleaning due to its strong penetration power.
The inclined plate 222a is formed to be inclined at an angle of 50 ° to 70 ° with respect to the horizontal plane, and upper and lower blocking baffles 222b and 222c are respectively formed on the upper and lower portions to prevent the sludge from rising. It is coated with a very hydrophobic material
The ultra-hydrophobic material is an energy-saving sewage treatment system, characterized in that the metal oxide fine particles selected from the group consisting of TiO2, SnO2, ZnO, WO3, Nb2O5, TiSrO3, Anatase-type TiO2. The method of claim 1,
Energy-saving sewage treatment system, characterized in that the treated water in the aeration area 210 is overflowed through the top of the partition 230 flows into the non-aeration area (220). The method of claim 2,
The non-aeration area 220 is provided with a vertical plate 224 in a vertical direction in a state spaced apart from the partition wall 230,
Energy-saving sewage wastewater treatment system, characterized in that the treated water flowing from the aeration area 210 flows downward through the inflow path 225 formed between the partition wall 230 and the vertical plate (224). The method of claim 3, wherein
The bottom surface of the non-aeration area 220 is formed to be inclined downward from the partition wall 230, the energy saving, characterized in that the sludge is collected and concentrated in the sludge collection hopper 226 formed in the distal end portion of the bottom surface Type sewage treatment system. The method of claim 1,
Energy-saving sewage and wastewater treatment system, characterized in that the pin-floc discharge pipe (900) for discharging the pin floc included in the upper water to the outside on one side of the membrane module (221). 6. The method of claim 5,
The reactor 100 is an energy-saving sewage treatment system, characterized in that a pair of first and second alternating reactors (100a, 100b) are arranged in parallel to communicate with each other by the outlet sleeve (110). The method according to claim 6,
Further, the first and second outflow equipments 310 and 320 are respectively provided with first and second outlet valves for allowing the treated water treated in the first and second alternating reaction tanks 100a and 100b to flow into the separation tank 200. Energy-saving sewage treatment system including. The method of claim 1,
The suction device 600 is connected to the separator module 221, the suction pipe 610 for sucking and discharging the final treated water separated by the separator 221a to the outside,
Energy-saving sewage water treatment system including a suction pump 620 is installed on the suction pipe 610 to adjust the suction pressure. The method of claim 1,
Energy-saving sewage water treatment system further comprises a hydrocyclone (500) is installed on the sludge conveying line 400 is a solid-liquid separation of sludge and filtrate in the interior by the pressure of the sludge conveying pump (410).

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