KR20190041701A - A biological pretreatment apparatus containing disk filter and a separation method therewith - Google Patents

Abstract

The present invention relates to a biological pretreatment apparatus comprising a mixing tank and a disk filter unit. In order to separate sludge in which organic matters are adsorbed formed in the mixing tank, the sludge in which organic matters are adsorbed is separated using the disk filter instead of a solid-liquid sedimentation separation apparatus being used. By using the disk filter instead of a conventional sedimentation type separation tank, the size of the solid-liquid sedimentation separation apparatus used in the conventional separation tank can be reduced. Also, by selectively controlling the disk filter having various pore sizes, the separation efficiency of the sludge in which the organic matters are adsorbed can be enhanced.

Description

TECHNICAL FIELD The present invention relates to a biological pretreatment apparatus and a biological pretreatment apparatus,

The present invention relates to a biological pretreatment apparatus (admixture tank and separation tank), in which a disk filter is used instead of a solid-liquid sedimentation separation apparatus used for separating sludge adsorbed on an organic matter formed in a mixing tank Separate the sludge with organic matter adsorbed.

In addition, the biological pretreatment apparatus according to the present invention can reduce the size of the liquid-phase sedimentation separation apparatus used in a conventional separation tank by adding a disk filter to the rear end of the conventional separation tank, The separation efficiency of the sludge adsorbed by the organic matter can be improved.

In addition, the separated organic sludge can be recycled back to the mixing tank to maintain a high coagulation efficiency. The COD (Chemical Oxygen Demand) or BOD (Biological Oxygen Demand) of raw water is previously measured in the mixing tank to determine the degree of organic matter adsorbed on the sludge By grasping in advance, the pore size of the disk filter to be used can be varied variously, and the sludge separation efficiency can be optimized.

As a result of the development of industry, rapid progress has been made in various technical fields. However, due to this, the discharge of sewage including various pollutants such as agriculture, industrial wastewater, industrial wastewater, industrial wastewater, Environmental pollution is becoming an important issue.

These kinds of sewage pollute the water quality of public water such as inland and coastal waters and urban small and medium rivers. Especially in recent years, due to rapid industrial development, population increase and population concentration of the city, The proportion of inorganic and organic components in wastewater is increasing.

Such wastewater contains high concentrations of organic matter such as COD (Chemical Oxygen Demand), BOD (Biochemical Oxygen Demand), SS (Suspended Substance), Nitrogen and Phosphorus and flows into rivers, As well as the destruction of ecosystems due to toxicity, which adversely affects the environment. Therefore, the wastewater is to be purified to a predetermined standard value or less by setting a certain standard.

In the meantime, conventional treatment methods for removing suspended particles in wastewater during the treatment of wastewater include chemical treatment, electrical treatment, filtration, membrane method and the like. Among the most typical treatment methods are coagulant ), It is known as the most common method so far that the surface properties of particles are changed by using an inorganic coagulant or an organic coagulant to form a floc and precipitate.

The basic process of the chemical treatment method using such coagulant is as follows. First, the colloid in the sewage water to be treated is neutralized using a metal salt (generally, iron or an aluminum compound) to undergo an aggregation step for producing micro flocs, and then subjected to a floc formation step for collecting and growing micro flocs. This can be done by adding a polymer to the micro flocs generated in the coagulation step. Thereafter, a step of generating processed digits is performed by separating sludge produced by precipitating flocs from the for-treatment water.

It is important to chemically treat the coagulant by improving the quality of the flocculant so that the formation of the flocs, the growth and the production of the sludge are efficiently performed because the capacity of the overall sewage treatment facility including the mixing tank and the settling tank is reduced, This is because it is directly related to the effect of facility cost reduction and maintenance / repair cost reduction. Therefore, there is a demand for a technique capable of achieving an excellent water treatment effect, such as reduction in facility cost, by improving the conventional chemical treatment method.

Patent Registration No. 10-1145049

Disclosure of Invention Technical Problem [8] Accordingly, the present invention has been made keeping in mind the above problems occurring in the prior art, and it is an object of the present invention to provide a sludge- And a semi-permanent disk filter is used to separate the sludge adsorbed on the organic matter.

In addition, by applying the disk filter unit to the biological pretreatment device, it is possible to effectively reduce the hydraulic retention time and site area as compared with the conventional sedimentation separation device, and to control the pore size of the disk filter included in the disk filter unit Thereby providing a biological pretreatment device and a method of operating the same, while flexibly controlling the hydraulic retention time and the sludge moisture content.

These and other objects and advantages of the present invention will become apparent from the following description of a preferred embodiment.

According to an aspect of the present invention, there is provided a biological pretreatment apparatus including: a receiving space for receiving water to be treated; And an outlet for discharging the water to be treated accommodated in the accommodation space to the outside, wherein the organic pollutants contained in the for-treatment water are flocked to form sludge Mixing tank; And a disc filter unit for separating the sludge contained in the for-treatment water discharged through the discharge port of the mixing tank.

The disc filter unit preferably has a pore size of 25 to 200 m, more preferably at least one disc filter having different pore sizes.

The mixing tank may further include a detector for measuring COD or BOD of the supplied untreated water. The COD or BOD value of the water to be treated measured by the detector may include sludge discharged from the mixing tank The water to be treated can be supplied to at least one disk filter included in the disk filter unit.

The sludge formed as a cake layer on the surface of the disk filter is subjected to a biological pretreatment process to remove the sludge from the surface of the disk filter. The thickness of the cake layer formed on the surface of the disk filter is increased.

The increase in the thickness of the cake layer on the disk filter surface causes an increase in the pressure difference between the disk filters. Therefore, when the increase in the differential pressure reaches about 20% It is preferable that the backwash water is supplied in the direction opposite to the direction in which the water is treated to desorb the sludge constituting the cake layer formed on the surface of the disk filter.

It is further preferable that the sludge desorbed by the backwash water is returned to the mixing tank again.

It is preferable that an agitator capable of agitating the incoming water to be introduced into the mixing tank to form the sludge by growing the organic contaminants contained in the for-treatment water by flaking, and it is preferable that at least two or more .

In addition, the stirrer may use an impeller type having a wing shape, and a perforated plate having a cavity having a diameter of 3 to 5 cm may be further provided between the plurality of stirrers.

Alternatively, a settling tank may be additionally provided between the mixing tank and the disk filter unit. In this settling tank, a part of the sludge generated in the mixing tank is previously settled so that the sludge separated in the solid- The backwash period can be reduced.

In another embodiment of the present invention, there is provided a biological pretreatment method, comprising: an influent step of supplying a for-treatment water to a mixing tank containing a receiving space for receiving the for-treatment water; Forming a sludge by growing an organic contaminant contained in the for-treatment water in the mixing tank in a flask; A discharging step of discharging the water to be treated including sludge in the mixing tank; And a solid-liquid separation step of supplying the discharged untreated water to the disk filter unit to separate the sludge contained in the for-treatment water.

Preferably, the disk filter unit includes a plurality of disk filters having different pore sizes, and the pore size has a pore size range of 25 to 200 m.

The mixing tank may further include a detector for measuring COD or BOD to measure COD or BOD of the water to be treated supplied from the inlet stage, Treated water containing sludge discharged from the mixing tank is supplied to at least one of the disk filters included in the disk filter unit according to the COD or BOD value of the treated water.

In the solid-liquid separation step, the for-treatment water containing sludge supplied to the disk filter unit is solid-liquid separated through a disk filter in the disk filter unit, and a cake layer is formed on the surface of the disk filter in this process.

And a recovery step of supplying the backwash water to the disk filter after the solid-liquid separation step, and desorbing the sludge formed as the cake layer on the surface of the disk filter and recovering the sludge to the mixing tank, A precipitation step in which a part of the sludge is precipitated through the settling tank, between the discharging step and the solid-liquid separation step.

The biological pretreatment apparatus according to the present invention can reduce the size of the liquid-phase sedimentation separation apparatus used in a conventional separation tank by adding a disk filter to the rear end of the conventional separation tank, It is possible to improve the separation efficiency of the sludge adsorbed by the organic matter and to reduce the initial investment cost, the automatic operation and the semi-permanent use.

In addition, the separated organic sludge can be recycled back to the mixing tank to maintain a high coagulation efficiency. The COD (Chemical Oxygen Demand) or BOD (Biological Oxygen Demand) of raw water is previously measured in the mixing tank to determine the degree of organic matter adsorbed on the sludge By grasping in advance, the pore size of the disk filter to be used can be varied variously, and the sludge separation efficiency can be optimized.

However, the effects of the present invention are not limited to those mentioned above, and other effects not mentioned can be clearly understood by those skilled in the art from the following description.

Figure 1 schematically depicts a conventional biological pretreatment device.
2 schematically shows a biological pretreatment apparatus according to an example of the present invention.
3 and 4 are views schematically showing an acid device according to an example.
FIG. 5 is a schematic view of a mixing tank provided with a stirrer and a perforated plate according to an example.
6 is a schematic view of an agitator according to an example.
7 schematically shows a biological pretreatment apparatus including a disk filter unit according to an example of the present invention.
FIG. 8 (a) is a schematic diagram showing the water to be subjected to solid-liquid separation through a disk filter, FIG. 8 (b) is a schematic diagram showing a state in which a cake layer is formed on the surface of the disk filter, 8 (c) schematically shows a process of discharging the cake layer of the sludge formed on the surface of the disk filter through the backwash water.
9 is a view schematically showing a settling tank according to an example.
10 (a) and 10 (b) are schematic views of an orifice tube according to an example.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. Prior to the description, terms and words used in the present specification and claims should not be construed as limited to ordinary or dictionary meanings and should be construed in accordance with the technical concept of the present invention. In the following description, well-known functions or constructions are not described in order to avoid unnecessarily obscuring the subject matter of the present invention.

Throughout this specification, when a member is " on " another member, this includes not only when the member is in contact with another member, but also when there is another member between the two members.

Throughout this specification, when an element is referred to as " including " an element, it is understood that it may include other elements as well, without departing from the other elements unless specifically stated otherwise.

The terms " first ", " second ", and the like are intended to distinguish one element from another, and the scope of the right should not be limited by these terms. For example, the first component may be referred to as a second component, and similarly, the second component may also be referred to as a first component.

It is to be understood that both the foregoing general description and the following detailed description of the present invention are exemplary and explanatory and are intended to provide further explanation of the invention as claimed. It should not be interpreted.

Fig. 1 schematically shows a conventional biological pretreatment apparatus 1 according to the prior art. As shown in FIG. 1, the conventional biological pretreatment apparatus 1 includes a mixing tank 10 for flushing and growing contaminants contained in the incoming water to be treated; And a sedimentation tank 20 for sedimenting and discharging the flocs introduced from the mixing tank 10 in the form of sludge.

In the mixing tank, organic matter adsorption using activated sludge and flocculant (Fe or Al) is performed, and in the settling tank, a process of solid-liquid separation of the sludge adsorbing organic matter proceeds. In the sedimentation tank, There is a problem of increase in residence time, site area, initial investment cost, and operation cost.

It is to be understood that this conventional biological pretreatment apparatus (which will be described in advance not to mean that the biological pretreatment apparatus referred to in this specification as the conventional art or existing art is known prior to the filing of the present invention) A biological pretreatment apparatus 100 according to an embodiment of the present invention is schematically shown in Fig.

The biological pretreatment apparatus (100) comprises: a receiving space (101) for receiving water to be treated; An inlet 102 for supplying water to be treated to the accommodation space 101 and an outlet 103 for discharging the water to be treated contained in the accommodation space 101 to the outside, A mixing tank 200 for growing sludge by growing the organic contaminants into a flock; And a disc filter unit 300 for separating the sludge contained in the for-treatment water discharged through the discharge port 103 of the mixing tank 200.

In the mixing tank 200, contaminants contained in the for-treatment water flowing into the water to be treated are formed and grown in the form of flocs, and the treated water discharged through the discharge port 103 is filled with sludge And the water to be treated including a solid phase in the form of sludge in the mixing tank 200 is contained in the solid phase of the disk filter unit 300 Liquid separation.

The mixing tank 200 may further include an acid device 150 at the bottom to form and grow contaminants contained in the water to be treated supplied into the mixing tank 200. The acid device 150 may function to supply bubbles into the accommodation space 101 of the blending tank 200. When the bubbles are supplied into the accommodation space 101, the microbes may be extracellular Polymeric Substance (EPS) is secreted, and Suspended solid (SS) is adsorbed on the floc or sludge. Through this, it is possible to effectively recover the organic matter, and to maximize the production amount of methane gas in the succeeding process (biological treatment process, B-stage, etc.).

The saturation device may be divided into a saturator type device and a mixer type device. The saturator type device includes a pressure dissolved chamber 111 therein, A pump 115 for supplying water to the saturator 112 through a water supply pipe 114 and a high-pressure air supply pipe 112 for supplying high-pressure air to the saturator 112 via the air supply pipe 113 And a spray nozzle 118 connected to the saturator 142 through the compressor 116 and the discharge pipe 117 to spray air with dissolved air to form bubbles. A plurality of spray nozzles 118 may be installed in the mixing chamber 200. The pair of spray nozzles 118 may be installed such that the sprayed bubbles collide with each other to form minute bubbles. (See Fig. 3).

The mixer type dissipating device includes a supply pipe 121 in which air and water are mixedly supplied, a pump 122 connected to the supply pipe 121 to form bubble water through pumping, And an injection nozzle 126 connected to the mixer 124 through a mixer 124 having a mixing chamber 123 and a discharge pipe 125 to form bubbles by discharging bubble water to the outside. The injection nozzles 126 are installed in the mixing chamber 200, and a plurality of the injection nozzles 126 may be installed so that the bubbles are collided with each other to form minute bubbles. (See Fig. 4).

In one embodiment, the mixing tank 200 may further include an agitator 130 for agitating the incoming water to be treated. The agitator 130 agitates the water to be treated, Allowing the material to grow into a flock (see FIG. 5).

The impeller type stirrer 130 is not particularly limited in shape, but the outer wing portion 132 preferably includes an inner wing portion (not shown) 131). By this, the water can be gathered by hand, and the water can be pushed out as much as possible in the desired direction as if the water is pushed out strongly, thereby maximizing the stirring effect Reference).

In addition, a plurality of stirrers 130 may be provided in the mixing tank 200. When a plurality of stirrers 130 are provided, a plurality of stirrers 130 having different blade diameters may be the same or different in diameter, but a plurality of stirrers 130 may be provided in the upper portion of the mixing tank 200, It is preferable to dispose the water to be treated so as to have a smaller diameter toward the side closer to the mixing bath 200. This is because the inflow water to be treated moves from the upper portion to the lower portion of the mixing bath 200 and the mixing efficiency can be increased due to the higher mixing speed.

The number of revolutions (G-value) of the wing of the stirrer 130 is not particularly limited and may be appropriately selected according to the size of the mixing and agglomeration scale or the size of the mixing tank 200, preferably 30 to 110 sec ^-1 and, more preferably, the number of revolutions of the blade diameter of the largest agitator 130 of the plurality of agitators 130 and 70 ~ 110sec ^-1, the number of revolutions of the blade diameter of the smallest agitator 130 30 ~ 50sec ^{- 1} < / RTI >

In one embodiment, the mixing tank 200 may include at least one perforated plate 140 between a plurality of agitators 130. In the case of one agitator 130, A perforated plate 140 may be provided. The plurality of cavities formed in the perforated plate 140 are not particularly limited and may be variously selected depending on the size of the perforated plate 140 and the size of the admixture tank 200. However, desirable.

In one embodiment, the blend tank 200 may have a plate-shaped baffle therein, and growth may be promoted when the bladders collide with the baffle. The number of baffles is not particularly limited, but it is preferable that at least three baffles are formed on one wall surface of the mixing tank 200 for the effect of the flask coagulation.

In one embodiment, the mixing bath 200 may include control means capable of controlling the stirring speed of the stirrer 130 according to the internal temperature and the amount of formed flocs. At this time, the control means controls at least one of a temperature sensor for measuring the upper and lower temperatures in the mixing tank 200, a particle counter for calculating the amount of the flocs, and a detector capable of measuring BOD or COD of the water to be treated It is preferable to operate in connection with the means.

The detecting means included in the mixing tank 200 is connected to the control unit to select a disk filter having a proper pore size from a plurality of disk filters existing in the disk filter unit 300 to be described later, Can be operated.

In one embodiment, the mixing tank 200 includes a flocculant supply unit (not shown) for supplying a flocculant containing a salt, a polymer material, or the like, which induces the formation and growth of the flocs, ). ≪ / RTI > The coagulant used in the present invention is a substance having a relatively small molecular weight and serves as a floc seed to bind with organic particles or inorganic particles in the water to be treated to form a flock.

Salt (salt) contained in the coagulant is an aluminum (Al) or iron (Fe) based metal salts _{(Al 2 (SO 4) 3} , Fe 2 (SO 4) 3, FeCl 3, Al 2 (OH) 3 Cl 2 Etc.), and it is more preferable to be an iron salt (FeM _n ) such as FeCl ₃ . High molecular (polymer) material to be included in the coagulant is poly-aluminum chloride _{(Polyaluminium chloride, [Al 2 (} OH) n Cl 6 -n] n), poly aluminum silicate sulfate (Polyalumium sulfate silicate, PASS, Al _a (OH) _b (SO 4) _c (SiO ₂ ) _d (H ₂ O) _x ), polyaluminum hydroxide chloride silicate, PACS, AlNa _x Si _y (OH) _z Cl _b ), polyamine and poly At least one of polyacrylamide (PAM) may be used. In particular, it is preferable that an anionic polymer material is included. Such an anionic polymer material is effective to promote flocculation, sedimentation and filtration.

In addition, inorganic coagulants such as aluminum salts and iron salts such as aluminum oxide, ferrous sulfate, ferric sulfate, ferric chloride, and aluminum chloride (PAC), polymer flocculants, acrylic polymers such as MT Aqua Polymer cationic polymer gel (AOA), Ammonia Oxidizing Bateria (AOB), and Nitrite Oxidizing Bacteria (NOB) can be used alone or in combination of two or more kinds of cationic polymers which swell in water and do not substantially dissolve in water. May also be used.

In addition, coagulant may be added in addition to the coagulant. Examples of the coagulant aid that can be used herein include clay, calcium hydroxide, a cation flocculant, an anionic flocculant and a nonionic flocculant.

The treated water passing through the mixing tank 200 can be supplied to the anaerobic digestion tank after the sludge is separated by solid-liquid separation through the disk filter unit 300. In this anaerobic digestion tank, anaerobic digestion of the ammonium-containing water generated in the anaerobic digestion tank is performed using anaerobic ammonium-oxidizing bacteria (Anammox), and the final water treatment is performed through a continuous batch type reaction tank in which only the bacteria are separated.

A plurality of disk filters having various pore sizes may be used in series or in parallel in the disk filter unit 300. The pore size of the disk filter may be selected within a range of 25 to 200 mm.

The disk filter unit 300 may be constructed so that the disk filters 301, 302, and 303 having different pore sizes are connected in parallel as shown in FIG. 7, A particle counter that is located inside the accommodation space 101 and calculates the amount of the flush contained in the for-treatment water, or a detector that can measure the BOD or COD of the water to be treated, The controller 402 controls the valve 402 to supply the water to be treated with a disk filter having an appropriate pore size.

For example, after a disk filter unit 300 having a pore size of 25 to 50 mm, a disk filter 302 of 50 to 100 mm and a disk filter 303 of 100 to 200 mm in parallel is provided , When the amount of the organic pollutants contained in the water to be treated supplied to the treated water receiving space 101 of the mixing tank 200 is small, the value of BOD or COD detected by the detecting device 401 is low And the size of the sludge formed by the organic contaminants is relatively small. Therefore, in the control unit 400, the water to be treated discharged from the mixing tank 200 is purged even in the disk filter unit 300 And is supplied to the disk filter 301 whose size is relatively small.

It is also possible to use not only the BOD or COD detector but also a particle counter for directly measuring the amount of the formed flocs in the water quality detection device 401 of the for-treatment water.

The solid-liquid separation process can be more effectively performed by measuring the amount of flocs generated in the water to be treated or the mixing tank supplied to the mixing tank and selecting the size of the disk filter to be solid-liquid separated in the subsequent process.

FIG. 8 shows the disc filter in which the solid-liquid separation process is performed in more detail. 8, the for-treatment water containing sludge supplied to the disk filter 301 is solid-liquid separated through the disk filter 301 to form the cake layer 310 on the disk filter surface.

As the sludge is formed as a cake layer on the surface of the disk filter 301, cake filtration can be performed by the cake layer on the surface of the disk filter, so that filtration and solid-liquid separation can be performed more precisely than the actual pore size . Therefore, it is very important to form the initial cake layer on the surface of the disk filter. For this purpose, as described above, the role of the controller for selecting a disk filter having a pore of an appropriate size according to the concentration and amount of the supplied floc sludge is very important do.

As the filtration by the sludge cake layer progresses, the pressure difference rP applied to the disk filter gradually increases. In the case of increasing to about 20%, it is preferable to perform backwashing for stable operation of the process. When the backwash water is supplied to the disk filter (Inside Out) in the direction opposite to the direction in which the for-treatment water passes through the disk filter (Outside In), the sludge formed on the surface of the disk filter, as shown in FIG. 8, .

At this time, it is preferable that at least a part of the sludge desorbed is not closed but is recovered to the mixing tank again. By supplying the desorbed sludge to the mixing tank 200 again for forming and growing the flocs, So that the formation of the flocs and the sludge growth time can be reduced. Also, all or a part of the sludge may be conveyed to the mixing tank 100 for circulation, thereby reducing the overall sludge discharge amount.

If necessary, a sedimentation tank 600 of the type shown in FIG. 9 may be additionally provided between the mixing tank 200 and the disk filter unit 300 constituting the biological pretreatment apparatus according to the present invention. In this case, it is possible to operate the sedimentation tank relatively small in comparison with the sedimentation tank according to the conventional technique shown in FIG. 1 and to reduce the amount of sludge in the solid-liquid separation performed in the disk filter unit 300 So that the backwash cycle for desorbing the sludge formed on the surface of the disk filter can be reduced.

That is, in the settling tank 600, the untreated water including the fl ow is introduced from the mixing tank 100, the settled water is settled and discharged in the form of a sludge, And a sludge discharge port 605 for discharging the sludge to the lower part of the filter unit 300 (see FIG. 9). Although the sedimentation tank 600 is not particularly limited, it is preferable that the overall appearance is a cylindrical or square pillar shape, and the lower part is formed to be inclined toward the vertical center axis so that the sludge is discharged to the outside.

In one embodiment, the settling tank 600 may include a circular orifice tube 610 at the bottom to deposit the flock effectively in sludge form. Here, the circle is a concept including a round shape and an oval shape. The orifice tube 610 may have a plurality of orifice holes 611. That is, when the flaps guided downward along the inner wall 601 of the settling tank 600 reach the circular orifice tube 610, they pass through the orifice hole 611 at a high speed and are precipitated as sludge to form a sludge outlet 605 Lt; / RTI >

More specifically, the flow Q, which is an amount that flows through a constant area over a period of time, can be expressed as a product of the cross-sectional area A and the flow velocity v, When passing through the orifice hole 611, the flow rate is the same, but the speed becomes very large as the cross-sectional area (orifice area) is sharply reduced. Thus, the flocs are deposited and discharged into the sludge as they pass through the orifice holes 611 at a very high rate.

In one embodiment, the number of circular orifice tubes 610 may be one or more than two, and the number of the orifice tubes 610 is not particularly limited and may be appropriately selected depending on the scale of the settling tank 600 or the amount of raw water to be settled have. Preferably, it may be two or three. When there are a plurality of circular orifice tubes 610, the average diameter of the orifice tubes 610 may be the same or different, and more preferably, a plurality of circular orifice tubes 610 having different average diameters may be disposed in the The sludge sedimentation rate can be further improved by arranging the sludge so as to have a smaller diameter from the upper side to the lower side. Here, the average diameter of the circular orifice tube 610 means the average length of the strings passing through the center of the orifice tube 610.

In one embodiment, the interior of the circular orifice tube 610 may include a branch tube 612. The branch tube 612 may include a plurality of orifice holes 611. The shape of the branch tube 212 is not particularly limited, but may be radially arranged in the circumferential direction from the center. That is, as shown in Fig. 10 (a), the inside of the circular orifice tube 610 is divided into three sections, or, as shown in Fig. 10 (b) Or alternatively arranged radially.

In one embodiment, the settling tank 600 may include a bend plate 620 to prevent floating of the sludge. The bent plate 620 may be manufactured in various shapes, but in order to effectively prevent the floating of the sludge, the bent plate 620 is preferably in the shape of a cone having an L-shaped cross section.

In one embodiment, the settling tank 600 may include a baffle 602 spaced a certain distance from the inner wall 601. When the for-treatment water containing flocs is supplied between the inner wall 601 of the sedimentation tank 600 and the baffle 602, the fluid including the flocs moves to the lower portion of the sedimentation tank 600 by gravity. At this time, the flow of the flux to the upper or central portion of the settling tank 600 is blocked by the installed baffle 602, and the flow direction can be stably guided to the lower side along the inner wall 601. At this time, the clean water from which the flakes have been removed can be discharged through the upper part of the settling tank 600.

In one embodiment, the settling tank 600 may include a guide plate 603 between the inner wall 601 and the baffle 602. As the guide plate disperses the flow of the fluid containing the flock (the water to be treated), it is possible to minimize the re-deposition of the sludge to be precipitated. The number of guide plates 603 is not particularly limited, but may be one to three.

The swash plate 604 may be provided at the distal end of the baffle 602 so that the fl ow or sludge can be stably directed toward the circular orifice pipe 610 without rising to the upper part of the settling tank 600. At this time, it is preferable that the end of the swash plate 604 is directed toward the center of the settling tank 600 in the inclined direction of the swash plate 604. [

Next, a biological pretreatment method of the water to be treated capable of improving the separation performance of the organic matter will be described. In describing the biological pretreatment method, the biological pretreatment apparatus 100 described above is used for the convenience of explanation, but the present invention is not limited thereto. Further, redundant description with respect to the biological preprocessing apparatus 100 is omitted.

According to an embodiment of the present invention, there is provided a biological pretreatment method including: an influent step of supplying a for-treatment water to a mixing tank including a receiving space for receiving the for-treatment water; Forming a sludge by growing an organic contaminant contained in the for-treatment water in the mixing tank in a flask; A discharging step of discharging the water to be treated including sludge in the mixing tank; And a solid-liquid separation step of supplying the discharged untreated water to the disk filter unit to separate the sludge contained in the for-treatment water.

It is preferable that the mixing tank further includes a detector for measuring COD or BOD, and the COD or BOD of the water to be treated supplied in the inflow step can be measured.

In order to effectively form and grow the contaminants contained in the for-treatment water flowing into the mixing tank, the stirring may be performed using an agitator. The agitator may be a plurality of impeller-type agitators having blades. When there are a plurality of stirrers, a perforated plate may be provided between each stirrer. At this time, the number of cavities formed in the perforated plate is not particularly limited, and may be variously selected according to the size of the perforated plate, the scale of the admixture, and the like, but it is preferable that the diameter is 3 to 5 cm.

It is also preferable that the disc filter unit includes a plurality of disc filters having different pore sizes, and the pore size has a pore size range of 25 to 200 m.

The discharging step may supply the for-treatment water containing sludge discharged from the mixing tank to at least one disk filter included in the disk filter unit according to the COD or BOD value of the water to be treated measured by the detecting unit , The solid-liquid separation step preferably separates the for-treatment water including the sludge supplied to the disk filter unit through the disk filter in the disk filter unit, and forms a cake layer on the surface of the disk filter.

After the solid-liquid separation step, when the pressure drop rP applied to the disk filter increases to 20% or more, the backwash water is supplied in the direction opposite to the direction in which the for-treatment water is supplied, It is preferable that at least a part of the desorbed sludge is recovered in the mixing tank.

A part of the sludge desorbed through the backwashing process is supplied to the mixing tank 200 again to recover the sludge. By using the sludge for the formation and growth of the sludge, it is possible to form a high-quality flask with improved size and density. And the settling time can be reduced. In addition, all or a part of the sludge may be returned to the mixing step and circulated, thereby reducing the overall sludge discharge amount.

Also, by injecting air bubbles during the growth of the flocs, it is possible to promote the secretion of EPS (Extracellular Polyeric Substance) of the microorganisms and to adsorb the organic substances and SS (suspended matter) components to the sludge so that the organic substances can be efficiently recovered. The effect of improving the production amount of methane gas in the biological treatment step can be obtained.

Optionally, it is also possible to add a precipitation step between the discharging step and the solid-liquid separation step, in which a part of the sludge is precipitated via a settling tank.

The precipitation step is a step of precipitating the flocs in the form of sludge and discharging the flocs out to the outside. Preferably, the flocs are passed through an orifice tube having a plurality of orifice holes in order to deposit the flocs effectively in a sludge form. In general, the flow rate Q which is a constant flow rate over a certain period of time can be expressed as a product of the pipe sectional area A and the flow velocity v. When the fl ux passes through a plurality of orifice holes formed in a circular orifice tube, But the speed becomes very large as the cross-sectional area (orifice area) is sharply reduced. Thus, the flocs can be deposited and discharged into the sludge as they pass through the orifice holes at very high rates.

The sludge dehydrating agent can be supplied to the sludge supplied to the mixing tank in the process of recovering the sludge. The sludge dehydrated by the sludge dewatering agent has an increased density, so that it is possible to grow a high quality flock with increased size and density of the flour at the mixing stage. The sludge dehydrating agent may be a polymer material, and preferably, a cationic polymer material may be used.

It is to be understood that the present invention is not limited to the above embodiments and various changes and modifications may be made by those skilled in the art without departing from the spirit and scope of the invention.

1, 100: biological pretreatment device 10, 200: mixing tank
20, 600: settling tank 101: accommodation space
102: inlet 103: outlet
150: Mount apparatus 111: Pressure-dissolved chamber
112: saturator 113:
114: water pipe 115: pump
116: compressor 117: discharge pipe
118: injection nozzle 121: feed pipe
122: pump 123: mixing chamber
124: Mixer 125:
126: jet nozzle 130: stirrer
131: inner wing 132: outer wing
140: perforated plate 142: saturator
300: Disk filter unit 301, 302, 303: Disk filter
400: control unit 401: detection device
601: inner wall 602: baffle
603: Guide plate 604: Swash plate
605: Sludge discharge port 610: Orifice tube
611: Orifice hole 612: Branch tube
620: Bent plate

Claims (17)

A receiving space for receiving the for-treatment water; And an outlet for discharging the water to be treated accommodated in the accommodation space to the outside, wherein the organic pollutants contained in the for-treatment water are flocked to form sludge Mixing tank; And
And a disk filter unit for separating the sludge contained in the for-treatment water discharged through the discharge port of the mixing tank. The method according to claim 1,
Wherein the disk filter unit has a pore size of 25 to 200 m in pore size. The method according to claim 1,
The mixing tank further includes a detector for measuring COD or BOD of the supplied water to be treated,
Characterized in that the disk filter unit comprises at least one disk filter having different pore sizes. The method of claim 3,
The biological pretreatment apparatus may be configured to supply the for-treatment water containing sludge discharged from the mixing tank to at least one disk filter included in the disk filter unit in accordance with the COD or BOD value of the water to be treated measured by the detection unit Characterized in that the biological pretreatment device. The method according to claim 1,
Wherein the for-treatment water containing sludge supplied to the disk filter unit is solid-liquid separated through a disk filter to form a cake layer on the disk filter surface. 6. The method of claim 5,
Wherein the sludge formed as a cake layer on the surface of the disk filter is desorbed by the backwash water supplied to the disk filter and recovered into the mixing tank. The method according to claim 1,
Wherein the mixing tank is equipped with a stirrer capable of stirring the incoming water to be introduced. 8. The method of claim 7,
Characterized in that the stirrer is an impeller type having at least two or more blades in the mixing tank. 9. The method of claim 8,
And a porous plate having a cavity with a diameter of 3 to 5 cm formed between the agitators. The method according to claim 1,
Wherein a sedimentation tank is additionally provided between the mixing tank and the disk filter unit. An inflow step of supplying the for-treatment water to a mixing tank including a receiving space for receiving the for-treatment water;
Forming a sludge by growing an organic contaminant contained in the for-treatment water in the mixing tank in a flask;
A discharging step of discharging the water to be treated including sludge in the mixing tank; And
And a solid-liquid separation step of supplying the discharged untreated water to the disk filter unit and separating the sludge contained in the water to be treated. 12. The method of claim 11,
Wherein the disk filter unit includes a plurality of disk filters having different pore sizes,
Wherein the pore size has a pore size range of 25 to 200 m. 12. The method of claim 11,
Wherein the mixing tank further includes a detector for measuring COD or BOD to measure COD or BOD of the water to be treated supplied in the inflow step, 14. The method of claim 13,
The discharging step may include supplying the for-treatment water containing sludge discharged from the mixing tank to at least one of the disk filters included in the disk filter unit according to the COD or BOD value of the water to be treated measured by the detector ≪ / RTI > 12. The method of claim 11,
Characterized in that the solid-liquid separation step comprises subjecting the for-treatment water containing sludge supplied to the disk filter unit to solid-liquid separation through a disk filter in the disk filter unit, and forming a cake layer on the surface of the disk filter Way. 16. The method of claim 15,
Further comprising a recovery step of supplying the backwash water to the disk filter after the solid-liquid separation step, and desorbing the sludge formed as the cake layer on the surface of the disk filter and recovering the sludge as the mixing bath. 12. The method of claim 11,
And a sedimentation step of precipitating a part of the sludge by passing the sedimentation tank between the discharging step and the solid-liquid separation step.

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