KR101990772B1 - Dissolved air flotation type wastewater processing apparatus with microbubble contacting part equipped with latitudinal distribution cone formed with hole - Google Patents

Abstract

The present invention relates to a floatation separation type sewage treatment apparatus having a microbubble contact portion equipped with a horizontal distribution cone having a distribution cone hole. Through the distribution cone hole, sewage and floc can flow smoothly in a longitudinal direction. Through a microbubble water supply pipe, microbubble water is supplied to the microbubble contact portion without pressure loss and agglomeration of microbubbles, while bringing a uniform distribution of microbubbles in the microbubble contact portion. Therefore, installation cost and maintenance cost due to power consumption are low.

Description

[0001] The present invention relates to a floating separation type wastewater treatment apparatus having a micro-bubble contact unit equipped with a horizontal distribution cone in which a distribution cone hole is formed,

The present invention relates to a wastewater treatment apparatus, and more particularly, to a floating separation wastewater treatment apparatus having a fine bubble contact portion equipped with a horizontal distribution cone formed with a distribution cone hole.

The floating separation type wastewater treatment apparatus floats floating oil pollutants in the dispersion medium such as sewage or wastewater to fine bubbles and floats up to the water surface where the dispersion medium and the air are in contact to remove the pollutant or the sludge adhering the pollutant from the water surface It is a water treatment device.

Examples of the floating separation method used in the wastewater treatment apparatus include a mechanical floating method, a pressurized floating method, an electrolytic floating method, and a microbiological floating method. Since the mechanical floating method is disadvantageous in that the floc may be destroyed due to severe turbulence, it is not suitable for flotation separation of the water source and secondary treated wastewater. In the case of the electrolytic floating method, It has a disadvantage in that a very large amount of electric power is required to generate decomposed fine bubbles and a scale is generated on the electrode plate for electrolyzing water. Therefore, in the case of secondary treated wastewater or water source, the majority of sedimentation and pressurized flooding methods are used in the majority.

The pressurized flotation method removes contaminants by buoyancy by reducing the total specific gravity of the contaminants by attaching them to the contaminants by generating micro bubbles of 100 μm or less. And it takes a lot of power to maintain the pressure at 4 to 6 atmospheres, which is very economical.

Meanwhile, in the conventional flotation type wastewater treatment apparatus, minute bubbles are discharged from a plurality of nozzles provided at regular intervals on the bottom surface of the minute bubble contact portion, so that minute bubbles are uniformly raised in the minute bubble contacting portion, However, in the process of discharging the air dissolved by the high pressure through a plurality of nozzles having a narrow outlet diameter through the branch pipe, the diameter of the bubbles is increased due to the fusion of the minute bubbles, so that the pressure loss is generated. There was a limit to increase the maintenance cost.

Korean Patent No. 1054087 Korea Patent No. 1722099

The present invention relates to an apparatus and a method for controlling a pressure loss and a pressure loss through a micro-catcher supply pipe without using a nozzle having a large power consumption, such as a pressurizing pump, a compressor and a pressurizing tank, It is possible to reduce the maintenance cost due to the installation cost and the power consumption by providing the fine bubble catcher with uniform distribution of the minute bubbles in the microbubble contact portion while supplying the fine bubble catcher without agglomeration of the fine bubbles, And to provide a floating separation type wastewater treatment device having a fine bubble contact portion equipped with a horizontal distribution cone having a distribution cone hole capable of smoothly running in the longitudinal direction.

The present invention relates to a mixing unit (10) for mixing flocculant with an incoming wastewater to generate flocs in the wastewater; A flocculating portion (20) for flowing wastewater passing through the mixing portion (10) and stirring to grow flocs in the wastewater; A partition wall 321 formed with a wastewater inlet port 31 communicating with the lower portion of the flocculation portion 20, two side partition walls 322 and 323 and a fine bubble guide plate Bubble contact portion 30 formed by being surrounded by the micro bubble contact portion 30; A fine particle catcher discharge unit 40 for supplying fine particle catchers in the bottom direction from the bottom of the minute bubble contacting unit 30 to the wastewater flowing into the wastewater inflow opening 31; The wastewater flows into the fine bubble contacting portion 30 together with the flock brought into contact with the micro bubble contacting portion 30 from the micro bubble contacting portion 30 and the flock brought into contact with the microbubble floats on the water surface by buoyancy to form a sludge layer A floating sludge separation tank (50); A floating sludge discharge unit 60 installed at an upper portion of the other side of the floating sludge separation tank 50 communicating with the minute bubble contacting unit 30 and spaced apart from the bottom to discharge the collected sludge; A floating sludge collector (70) installed on the water surface of the floating sludge separation tank (50) and collecting floating sludge; A treatment water temporary storage tank 80 in communication with a lower portion of the floating sludge separation tank 50 to store treated water from which sludge has been removed; And a process water reservoir (90) communicating with the upper portion of the process water temporary storage tank to store process water, the device comprising:

Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. A cone-shaped distribution cone 35 having a narrow longitudinal direction and a long width direction is formed on the bottom surface 34,

The fine particle catcher discharge unit 40 is provided with a fine particle catcher supply pipe 43 and vertically installed to discharge the fine particle catcher supply pipe 43 in the direction of the vertex of the distribution cone 35,
Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. The ratio of width to length is 1: 0.5 to 1: 2,
And a distribution cone hole (353) is formed in a side surface of the distribution cone (35) on the side of the partition wall (321) toward the minute bubble guide plate (33).

The present invention relates to an apparatus and a method for controlling a pressure loss and a pressure loss through a micro-catcher supply pipe without using a nozzle having a large power consumption, such as a pressurizing pump, a compressor and a pressurizing tank, It is possible to reduce the maintenance cost due to the installation cost and the power consumption by providing the fine bubble catcher with uniform distribution of the minute bubbles in the microbubble contact portion while supplying the fine bubble catcher without agglomeration of the fine bubbles, There is provided a floating separation type wastewater treatment apparatus having a fine bubble contacting portion equipped with a horizontal distribution cone having a distribution cone hole capable of smoothly running in the longitudinal direction.

FIG. 1 is a configuration explanatory view of a conventional flotation type wastewater treatment apparatus provided with a pressurizing pump, a compressor, a line mixer, and a pressurizing tank, and having a branch pipe and a plurality of nozzles in a fine catcher feed pipe.
Fig. 2 is a plan view of the fine bubble contacting portion of the conventional floating separation type wastewater treatment apparatus of Fig. 1;
FIG. 3 is an explanatory view of the configuration of a floating separation type wastewater treatment apparatus according to an embodiment of the present invention, which includes a fine particle catcher complex pump, an overpressure air separation tank, and only a fine particle catcher pipe without nozzles or branches.
FIG. 4A is a plan view (top) and a front view (bottom) of a conical distribution cone, FIG. 4B is a top view and a front view (bottom) (Top) and front view (bottom) of a cone-shaped distribution cone, FIG. 4d is a top view and a front view (bottom) of a distribution cone in which the busbars of an oblique ridge cone are concavely curved, (Upper) and a front view (lower) of a dispensing cone provided with a fine-gravity catcher guide plate on the fine bubble guide plate side of a dispensing cone having a concave curved bus bar of an inclined ridge cone, (Upper) and a front view (lower) of a distribution cone in which a fine catcher guide plate is provided on a fine bubble guide plate side of a distribution cone formed in a concavely curved shape and a fine catcher interference plate is formed on a partition wall side, This concave curved distribution cone (Top) and front view (top) and bottom view (bottom) of a distribution cone having a distributing cone having a distributor cone hole gradually increasing in the direction of the fine bubble guide plate from a partition cone to a distribution cone having a fine- to be.
5 is an enlarged front sectional view of the lower portion of the A-portion micro-bubble contacting portion of Fig.
Fig. 6 is a left side view of an enlarged bottom portion of the A-portion micro-bubble contacting portion of Fig. 3; Fig.
FIG. 7 is a plan view of the dispenser cone formed on the bottom surface of the fine bubble contacting portion of the floating separable wastewater treatment apparatus according to the embodiment of the present invention and the portion of the fine grab catcher supply pipe when viewed from the upper portion of the fine grab catcher.
8 is a front cross-sectional view of a fine-grained-catcher complex pump of the floating separation-type wastewater treatment apparatus according to the embodiment of the present invention.

Brief Description of the Drawings Fig. 1 is a structural explanatory view of a conventional flotation type wastewater treatment apparatus, and Fig. 2 is a plan view of a fine bubble contacting portion.

1 and 2, the floating separation type wastewater treatment apparatus according to the related art includes an admixture 10 having a rapid agitator 11 for mixing flocculant with incoming wastewater to generate flocs in the wastewater. A first flocculation tank 21 having a slow stirrer 211 for flowing wastewater that has passed through the mixing unit 10 to the bottom and stirring to grow flocs in the wastewater, And a second flocculation tank (22) communicating with the flocculation tank (12) and descending while further growing the flocs; A partition wall 321 formed with a wastewater inlet port 31 communicating with the lower portion of the flocculation portion 20, two side partition walls 322 and 323 and a fine bubble guide plate Bubble contact portion 30 formed by being surrounded by the micro bubble contact portion 30; A fine particle catching and discharging unit 44 for supplying fine particles to the wastewater flowing into the wastewater inflow opening 31 from the bottom of the fine bubble contacting unit 30; The wastewater flows into the fine bubble contacting portion 30 together with the flock brought into contact with the micro bubble contacting portion 30 from the micro bubble contacting portion 30 and the flock brought into contact with the microbubble floats on the water surface by buoyancy to form a sludge layer A floating sludge separation tank (50); A floating sludge discharge unit 60 installed at an upper portion of the other side of the floating sludge separation tank 50 communicating with the minute bubble contacting unit 30 and spaced apart from the bottom to discharge the collected sludge; A floating sludge collector (70) installed on the water surface of the floating sludge separation tank (50) and collecting floating sludge; A treatment water temporary storage tank 80 in communication with a lower portion of the floating sludge separation tank 50 to store treated water from which sludge has been removed; And a process water reservoir (90) communicating with an upper portion of the process water temporary storage tank to store process water,

The fine particle catcher discharge unit 44 includes an inflow pipe 441 for sucking treated water from the temporary storage tank 80, a pressurizing pump 442 for sucking treated water from the inflow pipe 441 and discharging the treated water at a high pressure, A line mixer 444 for mixing the pressurized treated water with the compressed air, a pressurized mixed water of pressurized treated water and compressed air to dissolve the air , A mixed water supply pipe (446) for transferring mixed water of the treated water and compressed air pushed to the lower portion of the minute bubble contacting portion (30) in the pressurizing tank, a plurality of minute branches (4461, 4462), and a plurality of fine-grained catcher supply nozzles (4463, 4464) provided at a predetermined interval in the plurality of branch pipes.

In the conventional flotation type wastewater treatment apparatus, the flocs grown in the flocculation portion 20 float in the process of flowing the wastewater into the microbubble contacting portion 30 and the floating sludge separation tank 50, Removed.

However, in the conventional floating separation type wastewater treatment apparatus, the air is dissolved in the treatment water in the pressurization tank 445, and a large-capacity pressurization tank 445 is required to increase the dissolution efficiency. Further, in order to accelerate dissolution of air, The diameter of the bubbles is increased due to the fusion of the minute bubbles in the process of discharging the air dissolved by the high pressure through a plurality of nozzles having a narrow diameter of the discharge port through the branch pipe, The efficiency is reduced, the installation cost is increased, and the maintenance cost is increased due to the high power consumption.

Hereinafter, the present invention will be described with reference to FIGS. 3 to 8. FIG.

3 is a schematic view of a floating separation type wastewater treatment apparatus according to an embodiment of the present invention having a fine particle catcher complex pump 41 and an overpressure air separation tank 42 and having only a fine particle catcher supply pipe 43 without nozzles or branches. 4A is a plan view (top) and a front view (bottom) of a conical distribution cone 35, and FIG. 4B is a plan view (top) and a front view of a tilted conical distribution cone 35. FIG. FIG. 4C is a plan view (upper) and a front view (lower) of the tilted cone-shaped distribution cone 35, and FIG. 4D is a view showing a distribution cone 4E is a plan view (top) and a front view (bottom) of the fine bubble guide plate 33 of the distribution cone 35 in which the busbars of the inclined ridge cone are concavely curved, (Upper) and a front view (lower) of the distribution cone 35 provided with the tilted cone, and FIG. 4 A top view (top view) of the distribution cone 35 in which the fine bubble guide plate 351 is provided on the fine bubble guide plate 33 side of the formed distribution cone 35 and the fine bubble trap plate 352 is formed on the partition wall 321 side and FIG. 4G is a front view (lower) of FIG. 4A. FIG. 4G shows a fine bubble guide plate 33 of the dispensing cone 35 in which the busbars of the tapered cone are concavely curved, A distributing cone 35 in which a distribution cone 353 gradually widened in the direction of the fine bubble guide plate 33 from the partition wall 321 is formed in the distribution cone 35 on which the fine particle trap interfering plate 352 is formed, Fig. 5 is a front sectional view of an enlarged view of the lower portion of the A-portion micro-bubble contacting portion 30 of Fig. 3, and Fig. 6 is a front elevational view of the A- 7 is a side view of the microbubble contact portion 30 of the floating separation type wastewater treatment apparatus according to the embodiment of the present invention formed on the bottom surface 34 Micropores distribution cone 35 and the micropores catcher supply pipe 43 is a plan view of the portion when seen from the upper contact catcher 30.

8 is a front cross-sectional view of the fine particle catcher composite pump 41 of the floating separation type wastewater treatment apparatus according to the embodiment of the present invention.

The flotation type wastewater treatment apparatus according to one embodiment of the present invention includes an admixture portion (10) for mixing flocculant into inflow wastewater to generate flocs in the wastewater; A flocculating portion (20) for flowing wastewater passing through the mixing portion (10) and stirring to grow flocs in the wastewater; A partition wall 321 formed with a wastewater inlet port 31 communicating with the lower portion of the flocculation portion 20, two side partition walls 322 and 323 and a fine bubble guide plate Bubble contact portion 30 formed by being surrounded by the micro bubble contact portion 30; A fine particle catcher discharge unit 40 for supplying fine particle catchers in the bottom direction from the bottom of the minute bubble contacting unit 30 to the wastewater flowing into the wastewater inflow opening 31; The wastewater flows into the fine bubble contacting portion 30 together with the flock brought into contact with the micro bubble contacting portion 30 from the micro bubble contacting portion 30 and the flock brought into contact with the microbubble floats on the water surface by buoyancy to form a sludge layer A floating sludge separation tank (50); A floating sludge discharge unit 60 installed at an upper portion of the other side of the floating sludge separation tank 50 communicating with the minute bubble contacting unit 30 and spaced apart from the bottom to discharge the collected sludge; A floating sludge collector (70) installed on the water surface of the floating sludge separation tank (50) and collecting floating sludge; A treatment water temporary storage tank 80 in communication with a lower portion of the floating sludge separation tank 50 to store treated water from which sludge has been removed; And a process water reservoir (90) communicating with the upper portion of the process water temporary storage tank to store process water, the device comprising:

Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. A cone-shaped distribution cone 35 having a narrow longitudinal direction and a long width direction is formed on the bottom surface 34,

The fine particle catcher discharge unit 40 is provided with a fine particle catcher supply pipe 43 and is vertically installed so that the fine particle catcher supply pipe 43 is discharged in the direction of the vertex of the distribution cone 35,

There is a major difference in the technical construction between the micro-bubble contacting portion 30 and the micro-catcher discharging portion 40 as compared with the conventional flotation type wastewater treatment device.

Hereinafter, the fine bubble contacting portion 30 will be described.

The wastewater inflow port 31 is a portion of the lower portion of the partition wall 321 that is not blocked by the partition wall 321 from the bottom to a predetermined height so as to communicate with the lower portion of the flocculation portion 20, And 323, as shown in FIG. The wastewater discharge port 31 is connected to the lower portion of the flocculation portion 20 at the lower portion of the partition 321 to increase the contact between the wastewater flowing into the flocculation portion 20 and the fine particle catcher supplied through the microfissure catcher supply pipe 43 May be 50 to 100%, preferably 60% or more, more preferably 70% or more of the entire width of the lower portion of the partition 321. If the width is too narrow, flocs formed in the flocculating portion 20 may be destroyed or the inflow amount of wastewater may be limited, which may reduce the treatment efficiency.

The widths of the two side partition walls 322 and 323 are smaller than the widths of the fine bubble introducing ports 31 from the wastewater inflow port 31 when the widths of the two side partition walls 322 and 323 are in the width direction. It is advantageous to increase the contact efficiency between the micro-catcher and the wastewater. In this case, the angle between the barrier ribs 321 and the side barrier ribs 322 or 323 may be 10 ° to 50 °, preferably 20 ° to 40 °. If the angle is too narrow, the advantage of increasing the contact efficiency of the wastewater can not be sufficiently exhibited. If the angle is too large, the bottom area of the minute bubble contacting portion 30 becomes narrow and the treatment efficiency can be reduced. The space between the partition wall 321 and the minute bubble guide plates 33 is increased and the installation area can be increased. More preferably, the width between the two side partition walls 322 and 323 can be widened at the predetermined angle and then kept constant at the same width as the width of the admixture, the flocculation portion, or the process water reservoir.

Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. The ratio of the width to the length is 1: 0.5 to 1: 2, preferably 1: 0.55 to 1: 1.5, more preferably 1: 0.6 to 1: 1. If the width is too long in the above range, the fine particle catcher discharged from the fine particle catcher supply pipe 43 does not reach the two side wall partitions 322 and 323, so that a dead area is generated in the minute bubble contact part 30, Is too long, the pressure for raising the flocs may be lost together with the wastewater, which may lower the wastewater treatment efficiency.

An imaginary line passing through the center of the fine-grab catcher supply pipe 43 coincides with a virtual line vertically penetrating the apex of the distribution cone 35 or a virtual line passing through the center of the fine- Line can be set to move in the direction of the minute bubble guide plate 33 by 5 to 50%, preferably 15 to 45%, more preferably 25 to 40% of the inner diameter length of the fine-grained catcher supply pipe 43 . If the moving distance in the direction of the minute bubble guide plate 33 is too short, the number of fine grains discharged to the partition wall 321 is too large to cause a vortex in the wastewater flowing in from the wastewater inlet 31, The mixing efficiency of the flock and the fine particle catcher can be reduced if the moving distance in the direction of the fine bubble guide plate 33 is too long.

The distribution cone 35 is preferably a conical shape of FIG. 4A, or a tilted conical shape of FIGS. 4C-4G rather than a tilted conical shape of FIG. 4B.

In the case of a conical shape, when the space between the partition wall 321 and the minute bubble guide plate 33 on which the wastewater inflow opening 31 is formed is in the longitudinal direction and the space between the two side partition walls 322 and 323 is the width direction, The length of the flow path through which the fine particle catcher discharged from the fine particle catcher supply pipe 43 is guided along the bus bar in the direction of the side partition walls 322 and 323 from the vertex of the cone to the bottom surface 34 is long And the length of the busbars in the longitudinal direction also increases together, the distribution of the micro-bubble catchers may not be uniform in the minute bubble contacting portion 30, which is relatively long in comparison with the length. desirable.

Also, although it is the case of the other cone having the same major axis, minor axis, and height, it is preferable that the apex of the cone is inclined conical shape shifted toward the partition 321. The degree of inclination is preferably from 20 to 95, preferably from 40 to 90, more preferably from 20 to 95 when the length of the major axis in the direction of the partition wall 321 from the vertex when the position of the vertex is not tilted is 100 So that a vertex is formed at a position between 60 and 85 degrees. When the degree of inclination is less than the above range, the length of the channel through which the micro-catcher discharged from the micro-catcher feed pipe 43 is guided along the bus bar in the direction of the micro catch guide plate 33 from the vertex to the bottom surface 34 is shortened, The efficiency of wastewater treatment due to the aggregation of minute bubbles is reduced. When the degree of tilting exceeds the above range, the number of micro-particles trapped in the distribution cone 35 toward the wastewater water inlet 31 becomes relatively large It may interfere with the flow of the wastewater and the floe, thereby reducing the floc rising efficiency and wastewater treatment efficiency.

The ratio of the minor axis to the major axis of the elliptical cone bottom is 1: 1.5 to 1: 4, preferably 1: 1.8 to 1: 3.8, more preferably 1: 2 to 1: 3.5. The length of the flow path through which the fine particles trapped in the fine particle catcher feed pipe 43 is guided along the bus bar in the direction of the side partition walls 322 and 323 from the vertex to the bottom surface 34 is shortened, The flow of the fine particles trapped in the side partition walls 322 and 323 toward the side partition walls 322 and 323 is strengthened and the fine bubbles are agglomerated and the efficiency of the wastewater treatment can be reduced .

It is preferable that the inclination of the bus bar of the distribution cone 35 gradually becomes gradually from the vertex toward the bottom surface 34, preferably the angle of the tangent of the bus bar located at the vertex is 60 ° to 90 °, preferably 70 ° to 85 ° °, the tangential angle of the bus bar in contact with the bottom surface is 0 ° to 50 °, and the tangent of the bus bar in the direction of the partition wall 321 is 25 ° to 50 °, preferably 30 ° to 45 °, , And the tangential line of the busbars in the direction of the fine bubble guide plate 33 is 0 ° to 35 °, preferably 10 ° to 25 °. As described above, the distribution cone having a concave curved cross section of the bus can take the flow of the micro catcher to the bottom surface 34 while minimizing the coagulation caused by the collision of the micro catcher.

A plurality of microcylinder guide plates 351 are formed along the busbars in the direction of the bottom surface 34 from the vertex to the side of the distribution cone 35 side of the microbubble guide plate 33, It is advantageous to distribute the fine grabber uniformly in a radial manner. The microcylinder catcher guide plate 321 may be formed perpendicular to the contact surface of the busbars from the vertex to the bottom surface 34 along the busbars or to a predetermined point therebetween, When the inner diameter of the supply pipe 43 is 100, it is formed at a height of 20 to 100, preferably 30 to 90, and more preferably 40 to 80.

A plurality of microcavity catcher plates 352 perpendicular to the busbars are provided on the side of the partition wall 321 side of the distribution cone 35 to be partially discharged in the direction of the wastewater water inlet 31 from the microcavity catcher supply pipe 43 It is preferable to distribute the fine catchers in the direction of the side partition walls 322 and 323 to prevent swirling of the incoming wastewater and to maintain the flocs. The microcavity trap plate may be perpendicular to the busbars, but may be inclined 15 to 45 degrees below both sides with respect to the center. The height of the micro catch trapping plate 322 is set to a height of 10 to 60, preferably 15 to 50, and more preferably 20 to 40, when the inner diameter of the micro catch catcher supply pipe 43 is 100.

A distribution cone hole 353 is formed on the side of the partition wall 321 side of the distribution cone 35 at the side of the fine bubble guide plate 33 side so that the flow of the wastewater and the floc by the distribution cone 35, Can be smoothly made in the longitudinal direction. The distribution cone hole 353 is formed so as to be wider in the direction of the fine bubble guide plate 33 from the partition wall 321. The entrance of the distribution cone hole 353 formed on the side wall of the partition wall 321 is formed on the side of the fine bubble guide plate 33 At least one of the width and the height is formed smaller than the outlet of the formed distribution cone hole 353. More preferably, the lower end of the inlet or outlet of the distribution cone 353 is in contact with or very close to the bottom surface 34, and the width and height gradually increase from the inlet to the outlet.

When the length from the partition wall 321 formed with the wastewater inflow opening 31 to the fine bubble guide plate 33 is 100 in the longitudinal direction, the distal end position of the microfeiter catcher supply pipe 43 is the center in the width direction, The imaginary line passing through the center of the fine particle catcher supply pipe 43 is 10 to 30 positions, preferably 15 to 25 positions. When the height of the wastewater inlet 31 is 100, The height from the bottom of the distal end of the micropore catcher supply pipe 43 is 100 to 120, preferably 105 (when the height of the distribution cone 35 is 100), the height is 80 to 100, preferably 85 to 95, Lt; / RTI >

The height of the dispensing cone 35 is 250 to 750 mm and the height of the distal end of the micro-catcher supply pipe 43 is 300 to 900 mm at the bottom surface 34 At this time, the height of the partitions 321, 322, and 323 from the bottom may be about 2 to 4.5 m.

The minute bubble guide plate 33 may be formed at an angle of 30 ° to 60 °, preferably 40 ° to 55 ° inclined from the bottom. The fine bubble guide plate 33 may be formed at a predetermined angle from the bottom to the distal end. Preferably, the angle of the bottom portion is relatively high and the angle of the distal portion is relatively low within the above range, And may be formed in a curved shape within the above range. In the case of the fine emitter discharging portion 44 of FIG. 2 in which a branch pipe and a plurality of nozzles are formed in a wide area of the bottom of the conventional micro bubble contacting portion 30, The flocs can be easily raised even when the inclination of the fine bubble guide plate 33 exceeds 60 ° or further vertically. However, in the case of the present invention, the micro- It is necessary to lower the angle below the upper limit value so that the floc can be raised while easily riding on the guide plate 33. However, if the angle of the minute bubble guide plate 33 is too low, the distance to the surface of the water becomes too long, which may make it difficult to raise the flocs.

The height of the minute bubble guide plate (33) is preferably 50 to 70% of the height of the wastewater of the minute bubble contacting portion (30).

Hereinafter, the fine particle catcher discharging unit 40 will be described.

The fine particle catcher discharge unit 40 includes an inflow unit 411 through which the treated water and air are supplied, a divided water supply unit 412 through which the treated water extending downward from the inflow unit 411 flows, A rotating lattice 413 provided in the replenishing section 412 for dividing the processing water and air while mixing them to form a fine particle collector by a partition plate 4131 rotating and spaced apart at a predetermined interval, An inner space 4143 formed on the outer circumferential surface of the inner space 4143 and having a diameter increasing and decreasing toward the upper side and an inner diameter 4143 formed on the outer circumferential surface of the inner space 4143; And a discharge section (414) including a protruding blocking plate (4142);

A mixed water supply pipe 421 for supplying the mixed water of the fine catcher and the coagulated foam water discharged from the discharge port 4141 of the fine particle catcher complex pump 41 and a pressure control valve 422 and an overpressure air discharge pipe 423, An overpressure air separation tank (42) equipped with a pressure sensor; And

And a fine particle catcher supply pipe (43) for discharging a fine pressure catcher of a predetermined pressure and a predetermined size from the overpressure air separation tank (42).

The air in the inlet 411 may be introduced together with the suction pressure of the treated water through the air inlet pipe 4111. Furthermore, an air inflow inlet pipe 4112 may be installed from the air inflow pipe to the inlet of the partitioning part 412 to more effectively introduce the air.

The fine particulate composite pump 41 sucks the treated water and air into the divided part 412 having a flow path narrower than the inflow part 411 by the rotation of the rotating lattice 413 formed with the partitioning plate 4131, The water and the air are divided while being mixed, and the resulting fine particle gun is transferred to the discharge portion 414 at a high pressure.

The fine particle collector generated by the fine particle catcher complex pump 41 is divided into fine bubbles smaller than a predetermined size and fine bubbles larger than a predetermined size by a discharge unit 414 having an inner space 4143 and a blocking plate 4142 The air exceeding the predetermined pressure is discharged to the gas by the pressure control valve 422 in the excess pressure air separation tank 42, Only the micro-particles trapped in the micro-particle trap feed pipe 43 is discharged. At this time, since the fine particle catcher supply pipe 43 is not provided with a separate branch pipe or a plurality of nozzles, the fine particle catcher can be supplied into the water without agglomeration of the minute bubbles or pressure loss.

The inner space 4143 of the discharge portion 414 extends upward from the partitioning portion 412 and increases in diameter toward the upper side and is formed to be decreased. The inner surface is curved and preferably spherical. When the processed water and air are mixed while being split by the rotation of the partitioning plate 4131 and the rotation grid 413 and the generated fine particle catcher is discharged into the inner space 4143, 7, and moves along the inner wall of the inner space 4143 while being hit by the blocking plate 4142 while being cohered with each other, so that the fluid is mixed with the inner wall of the inner space 4143, The fine bubbles are discharged from the partitioning part 412, passed through the center of the inner space 4143, and then discharged to the discharge port 4141. Therefore, the micro-sized catcher discharged from the partitioning part 412 moves through the flow path separated from the internal space 4143 of the discharge part 414 according to the size of the minute bubbles, and is discharged together with the discharge port 4141. That is, the fine particle catcher discharged to the discharge port 4141 coagulates while rotating toward the inner wall of the inner space 4143 and the minute bubbles smaller than the predetermined size moving to the center of the inner space 4143, do.

The height of the blocking plate 4142 is 5 to 40%, preferably 10 to 30% of the diameter of the spherical inner space 4143. If the height of the blocking plate 4142 is too low, the inner wall of the inner space 4143 may be discharged together with a minute particle less than a predetermined size which moves to the center before sufficiently agitating and rotating. If the height of the blocking plate 4142 is too high, the amount of fine bubbles agglomerated to a predetermined size or larger is relatively increased while rotating the inner wall of the inner space 4143, The efficiency of generation of micro-bubbles to generate bubbles and the power consumption reduction effect are reduced.

The height of the blocking plate 4142 is a truncated cylindrical shape with a high height in the rotating direction of the rotating lattice 413 and a low height in the opposite direction, It is more preferable to increase the saving effect.

The diameter of the spherical inner space 4143 is 3 to 6 times, preferably 4 to 5.5 times the inner diameter of the flow path of the partition 412 formed around the rotation grating 413. When the diameter of the spherical inner space 4143 is out of the above range, And the effect of reducing power consumption is reduced.

The flow path inner diameter of the inflow portion 411 is 2 to 4 times, preferably 2.5 to 3.5 times the inner diameter of the flow path of the partition 412 formed around the rotation grating 413, and below the lower limit, There is a limit to the increase of the discharge pressure of the fine particles discharged from the pump 41. When the upper limit is exceeded, a load is generated in the pump, so that the size and the capacity of the pump may be increased.

The treated water is sucked and supplied to the inlet 411 of the fine particle catcher complex pump 41 at a pressure of 0.1 to 0.6 bar, preferably 0.2 to 0.5 bar, and the air is supplied at a flow rate of 3 to 10% And the number of revolutions of the rotary grid 413 is 40 to 60 Hz, preferably 50 to 60 Hz. When the number of revolutions of the rotary grid 413 is out of the range, There is a limit in increasing the discharge pressure of the fine particle catcher and it is difficult to adjust the pressure discharged from the fine particle catcher complex pump 41 to 2 to 6 bar, preferably 3 to 5 bar.

The pressure regulating valve 422 of the overpressure air separation tank 42 may be set to 2 to 6 bar, preferably 3 to 5 bar. Since the micro-bubble catcher feed pipe 43 of the present invention is directly discharged to the minute bubble contact unit 30 without any pressure loss through the branch pipe or a plurality of nozzles, the pressure set by the pressure control valve 422 of the over- Is substantially the same as the pressure discharged from the fine-particle catcher supply pipe (43).

The micro-catcher supply pipe 43 supplies micro-catchers to the wastewater flowing into the wastewater inflow opening 31 in the bottom direction from the bottom of the micro-bubble contacting portion 30. The fine-particle catcher supply pipe 43 is a pipe for supplying the fine-particle catcher in the bottom direction without providing a separate branch pipe or a plurality of nozzles in the minute bubble contacting portion 30.

On the other hand, the bottom of the floating sludge discharge unit 60 may be inclined from the bottom of the fine bubble guide plate 33 toward the temporary storage tank 80. The inclination is preferably 2 DEG to 5 DEG. In the floating sludge separation tank 50 and the treated water temporary storage tank 80, the settling sludge blocking wall 81 is installed perpendicular to the bottom surface at a height of 5 to 30% of the height of the partition wall 321, It is advantageous to block the inflow of sludge.

Hereinafter, the present invention will be described in more detail with reference to examples. It will be apparent, however, to those skilled in the art that these embodiments are for describing the present invention in more detail, and that the scope of the present invention is not limited thereto.

Example 1

Referring to the plan view of the minute bubble contacting portion 30 of Fig. 7, the width to length ratio of the fine bubble contacting portion 30 is 1: 1.3, the width is 2.4 m, the length is 3.2 m, 8, the fine-particle-containing complex pump 41 shown in Fig. 8, the pressure-exceeding valve 40 shown in Fig. 8, and the pressure- An air separation tank (42); And a fine-particle catcher supply pipe (43). The height of the wastewater of the minute bubble contacting portion 30 was 2.1 m.

The treated water is supplied to the inlet 411 of the fine particle catcher complex pump 41 at a rate of 125 L / min at a pressure of 0.4 bar. The air is sucked at 10 L / min, and the rotation of the rotating lattice 413 The pressure control valve 422 of the overpressure air separation tank 42 was set to 4 bar so that the microcavity catcher of 4 bar was discharged to the microcavity catcher supply pipe 43.

The fine bubble discharging pipe 43 was installed at an inner diameter of 40 mm, in a direction perpendicular to the bottom at a height of 0.6 m from the partition wall 321 toward the fine bubble guide plate 33 and at a height of 0.41 m from the bottom.

4c, the distribution cone 35 has a height of 0.4 m, a major axis of 1.0 m and a minor axis of 0.4 m, and the apex of the distribution cone 35 is 0.3 in the direction of the minor axis of the partition wall 321 at the virtual vertex when the cone is not tilted. m was installed so as to come to the moved position.

Further, the virtual center line of the fine bubble discharging pipe (43) is arranged to move in the direction of the fine bubble guide plate (33) by 15 mm more than the vertex of the distribution cone (35).

Example 2

The distributing cone 35 has a height of 0.4 m in the shape of Fig. 4f, a major radius of 1.0 m, a minor radius of 0.4 m, and the apex of the distributing cone 35 is tilted The microcylindrical guide plate 351 is tilted so as to come to a position shifted by 0.3 m in the radial direction of the partition wall 321 and the microcylindrical guide plate 351 is radially moved toward the minute bubble guide plate 33 by 30 mm And installed vertically on the contact surface.

The inclination of the tangent to the vertex of the distribution cone 35 was 80 ° and the slope of the bus bar contacting the bottom surface 34 was 20 ° for the fine bubble guide plate 33 and 45 ° for the partition 321.

Example 3

The distributing cone 35 has a height of 0.4 m in the shape of Fig. 4g, a major axis of 1.0 m, a minor axis of 0.4 m, and the apex of the distribution cone 35 is tilted The microcylindrical guide plate 351 is tilted so as to come to a position shifted by 0.3 m in the radial direction of the partition wall 321 and the microcylindrical guide plate 351 is radially moved toward the minute bubble guide plate 33 by 30 mm And installed vertically on the contact surface.

The inclination of the tangent to the vertex of the distribution cone 35 was 80 ° and the slope of the bus bar contacting the bottom surface 34 was 20 ° for the fine bubble guide plate 33 and 45 ° for the partition 321.

The lower end of the inlet formed on the partition wall 321 side of the distribution cone 35 is in contact with the bottom surface 34 and has a height of 0.1 m and a width of 0.3 m and a lower end of the outlet formed in the micro- ), And the height was 0.18 m and the width was 0.6 m.

Comparative Example 1

The fine bubble contact unit 30 is constructed in the same manner as the second embodiment except that the dispenser cone 35 is not provided on the bottom surface 34 and the fine bubble catcher discharged from the fine bubble supply pipe 43 is directly connected to the bottom surface 34 Respectively.

Comparative Example 2

4b, the height of the distribution cone 35 is 0.4 m and the radius thereof is 0.4 m. The vertex point of the distributing cone 35 is the same as that of the imaginary vertex point when the cone is not inclined And was inclined so as to be located at a position shifted 0.3 m in the direction of the partition wall 321.

And a virtual center line of the fine bubble discharging pipe (43) is located at the center of the apex of the distribution cone (35).

Comparative Example 3

4b, the height of the distribution cone 35 is 0.4 m, and the radius thereof is 0.8 m, and the vertex of the distributing cone 35 is the same as that of the first embodiment except for a virtual vertex point when the cone is not inclined And was inclined at a position of 0.3 m in the direction of the partition wall 321.

And a virtual center line of the fine bubble discharging pipe (43) is located at the center of the apex of the distribution cone (35).

Comparative Example 4

1, a pressurizing pump 442, a compressor 443 for supplying compressed air to the pressurized treated water conveying pipe, and a pressurizing pump 442 for pressurizing the pressurized treated water conveying pipe are installed in the floating separation type wastewater treatment apparatus having the fine bubble contacting portion 30 of the same specification as Embodiment 1, A line mixer 444 for mixing the pressurized treated water with the compressed air, a pressurizing tank 445 for pressurizing the mixed water of pressurized treated water and pressurized air to dissolve air, a fine bubble contacting portion 30 A mixed water supply pipe 446 for transferring mixed water of the treated water and compressed air pushed to the lower portion of the mixed water supply pipe, two branch pipes 4461 and 4462 branched from the mixed water supply pipe, The fine bubble discharging portion 44 composed of eight fine catcher supplying nozzles 4463 and 4464 was installed at a height of 0.1 m from the bottom.

Experimental Example 1: Microbubble mean diameter and average bubble quantity

In the flotation type wastewater treatment apparatuses of Examples 1 to 4 and Comparative Examples 1 to 4, the water surface on both side edges of the partition wall 321 of the microbubble contacting portion, the microbubble diameter of the water surface on both side edges of the distal end of the microbubble guide plate 33, The bubble quantity was measured, and the average of these values was shown in Table 1 below.

division Average diameter (占 퐉) Average number of cells (ml / ml) Example 1 24 3,105 Example 2 23 3,412 Example 3 20 4,455 Comparative Example 1 28 1,912 Comparative Example 2 27 2,323 Comparative Example 3 30 1,820 Comparative Example 4 30 2,340

Experimental Example 2: Wastewater Treatment Efficiency

The treatment efficiencies of the wastewater were compared using the floating separation type wastewater treatment apparatuses of Examples 1 to 4 and Comparative Examples 1 to 4. The total wastewater entering (T-P) was 0.807 mg / L and the suspended material was 4.4 mg / L. The efficiency of wastewater treatment is shown in Table 2 below as a percentage of the total phosphorus or suspended matter reduction in treated wastewater treated wastewater from treated wastewater or spent wastewater.

division Total phosphorus treatment efficiency (%) Effluent treatment efficiency (%) Example 1 86 42 Example 2 88 49 Example 3 92 68 Comparative Example 1 80 19 Comparative Example 2 83 28 Comparative Example 3 79 11 Comparative Example 4 79 8

Experimental Example 3: Power Consumption

The average power consumption per day was averaged over seven days using the flotation type wastewater treatment apparatuses of Examples 1 to 4 and Comparative Examples 1 to 4, and the daily average power consumption was calculated and shown in Table 3.

division Average daily power consumption (kWh) Example 1 90 Example 2 80 Example 3 80 Comparative Example 1 100 Comparative Example 2 100 Comparative Example 3 100 Comparative Example 4 150

10: Admixture 11: Rapid agitator
20: agglomerating part 21: first agglomeration tank 211: slow agitator
22: Second coagulation tank
30: minute bubble contact portion 31: wastewater inlet 321: partition wall
322, 323: Lateral bulkhead 33: Fine bubble guide plate 34:
35: Distribution cone 351: Microscope catcher guide plate 352: Microscope catcher interferer plate
353: distribution cone hole
40, 44: minute bubble discharging portion
41: Micro-fine catcher complex pump 411:
4111: Air inlet pipe 4112: Air inlet inlet pipe
412: partitioning part 413: rotating lattice 4131: partition plate
414: discharge part 4141: discharge port 4142:
4143: Interior space
42: overpressure air separation tank 421: mixed water supply pipe
422: Pressure regulating valve 423: Excess pressure air outlet pipe
43: Micro-catcher feeder
441: Inflow pipe 442: Pressurizing pump 443: Compressor
444: Line mixer 445: Pressurizing tank 446: Mixed water supply pipe
4461, 4462: branch 4463, 4464: nozzle
50: floating sludge separation tank
60: floating sludge discharge portion
70: Floating sludge collector
80: treated water temporary storage tank 81: settling sludge blocking wall
90: treated water storage tank

Claims (13)

(10) for mixing flocculant into the incoming wastewater to produce flocs in the wastewater; A flocculating portion (20) for flowing wastewater passing through the mixing portion (10) and stirring to grow flocs in the wastewater; A partition wall 321 formed with a wastewater inlet port 31 communicating with the lower portion of the flocculation portion 20, two side partition walls 322 and 323 and a fine bubble guide plate Bubble contact portion 30 formed by being surrounded by the micro bubble contact portion 30; A fine particle catcher discharge unit 40 for supplying fine particle catchers in the bottom direction from the bottom of the minute bubble contacting unit 30 to the wastewater flowing into the wastewater inflow opening 31; The wastewater flows into the fine bubble contacting portion 30 together with the flock brought into contact with the micro bubble contacting portion 30 from the micro bubble contacting portion 30 and the flock brought into contact with the microbubble floats up on the water surface by buoyancy to form a sludge layer A floating sludge separation tank (50); A floating sludge discharge unit 60 installed at an upper portion of the other side of the floating sludge separation tank 50 communicating with the minute bubble contacting unit 30 and spaced apart from the bottom to discharge the collected sludge; A floating sludge collector (70) installed on the water surface of the floating sludge separation tank (50) and collecting floating sludge; A treatment water temporary storage tank 80 in communication with a lower portion of the floating sludge separation tank 50 to store treated water from which sludge has been removed; And a process water reservoir (90) communicating with the upper portion of the process water temporary storage tank to store process water, the device comprising:
Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. A cone-shaped distribution cone 35 having a narrow longitudinal direction and a long width direction is formed on the bottom surface 34,
The fine particle catcher discharge unit 40 is provided with a fine particle catcher supply pipe 43 and vertically installed to discharge the fine particle catcher supply pipe 43 in the direction of the vertex of the distribution cone 35,
Bubble contact portion 30 is formed in the width direction between the partition wall 321 formed with the wastewater discharge port 31 and the fine bubble guide plate 33 in the longitudinal direction and between the two side wall portions 322 and 323 in the width direction. The ratio of width to length is 1: 0.5 to 1: 2,
Wherein a distribution cone (353) is formed on a side of the partition wall (321) side of the distribution cone (35) to a side of the minute bubble guide plate (33) side. delete delete delete delete delete delete delete delete The method according to claim 1,
The inlet formed on the side of the partition wall (321) side of the distribution cone (351) is smaller in at least one of the width and height than the outlet formed on the side of the fine bubble guide plate (33) side. Wastewater treatment device. delete The method according to claim 1,
The height of the wastewater inlet 31 is 300 to 800 mm,
The height of the distribution cone 35 is 250 to 750 mm,
Wherein a height of the distal end of the micro-catcher feed pipe (43) is 300 to 900 mm above the bottom surface (34). delete

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