KR102006354B1 - Mixing-liquid transfer apparatus having scum removing and chemical solution dispensing input function and wastewater treatment method using inner circulation type sequencing batch reactor having the same - Google Patents

Abstract

The present invention relates to chemical solution transferring and stirring equipment having functions of removing scum and dispersing and injecting the chemical solution, which is capable of removing scum or dispersing and injecting an injected coagulating chemical solution to a reaction tank by using a negative pressure generated in a chemical solution transferring and stirring process; and a water treatment method using an internal circulation-type sequencing batch reaction apparatus including the same. Specifically, the equipment which is installed in one or more reaction tanks selected from two or more reaction tanks to transfer a reaction solution of an adjacent other reaction tank, includes: a driving motor which applies a rotational force; an impeller which is connected to a rotary shaft of the driving motor to be rotationally interlocked; a negative pressure space which is formed between the impeller and the driving motor and in which the negative pressure is generated by rotation of the impeller; a first guide unit which includes a first guide pipe formed in a pipe shape and accommodating the impeller, a plurality of connection rods installed to be spaced apart from one another along a circumferential direction on one side of the guide pipe facing the negative pressure space and connected to the driving motor, and an opening unit formed by a separation space between the connection rods; a second guide unit which includes a second guide pipe formed in a pipe shape with the diameter larger than the diameter of the first guide pipe, and connected to the other side of the first guide pipe so that a reaction solution is flown in through a gap between the second guide pipe and the first guide pipe; and a chemical solution transfer unit which allows the reaction solution received in an adjacent other reaction tank to be transferred to the negative pressure space.

Description

Mixing-liquid transfer apparatus having scum removing and chemical solution dispensing input function and wastewater treatment method using inner circulation type sequencing batch reactor having the same}

The present invention relates to a liquid transfer stirring apparatus for performing a liquid transfer between each reaction tank in a continuous batch activated sludge method, and a water treatment method using the same, and more specifically, to remove scum by using a negative pressure generated in the liquid transfer stirring process of the apparatus or The present invention relates to a liquid transfer stirring device having a scum removal and chemical liquid dispersing input function capable of dispersing the injected flocculated chemical liquid into a reaction tank and an internal circulation type continuous batch reaction device having the same.

Water treatment refers to the conversion of contaminants such as nitrogen, phosphorus and organic substances in water into stabilized substances through biological methods using microorganisms or chemical methods using chemicals.

Since biological methods have advantages over chemical methods in terms of the generation of by-products after treatment and the cost of treatment, biological methods dominate most of the general water treatment technologies, and various complex treatment methods have recently been developed. .

Representatively, the JASSFR-SBR method using the step-injected SBR reactor (liquid transfer stirring device) combined with the whole anaerobic tank and the natural flotation discharge system or the MBR method using the membrane bioreactor were proposed. Due to fluctuations in the quality of the water, scum in the reactor has been generated a lot.

The generation of scum causes a decrease in the efficiency of nitrogen treatment and increases the SS in the discharged water, which weakens the quality of the discharged water. Therefore, a separate facility is installed in each reactor to remove scum. .

On the other hand, T-N and T-P standards are being strengthened due to the strengthening of legal water quality, and in order to satisfy these standards, chemicals are added to react with the reaction solution during biological water treatment.

In this case, in order to add stable chemicals and maintain high reactivity, the reaction liquid of the reaction tank and the injected chemicals must be completely combined, but in the case of agglomerated chemicals, a separate dispersion facility and agitation are used to induce stable bonding with the reaction liquid. Since each facility must be provided, the cost of the facility increases, as well as the maintenance cost for operating it.

Republic of Korea Patent Publication No. 10-2010-0129642 (2010.12.09.)

Accordingly, an object of the present invention is to remove scum by using the negative pressure generated during the liquid transfer stirring process of the device and the liquid transfer stirring device having a scum removal and chemical liquid dispensing function to disperse the injected flocculation chemicals into the reactor And it is to provide a water treatment method using an internal circulation type continuous batch reactor having the same.

The liquid transfer stirring apparatus having the scum removing and chemical liquid dispensing function of the present invention for solving the above-mentioned problems is installed in one or more reaction tanks selected from two or more reaction tanks, the apparatus for transferring the reaction liquid of the other reaction tank, rotational force A driving motor to give; An impeller connected to the rotating shaft of the driving motor and interlocked with the rotating shaft; A negative pressure space formed between the impeller and the driving motor, the negative pressure space being generated by the rotation of the impeller; It is formed by a plurality of connecting rods and spaced space between the connecting rods installed in the circumferential direction on one side of the first guide tube for receiving the impeller in a tubular shape and the first guide tube facing the negative pressure space and connected to the drive motor. A first guide part including an opening portion; A second guide part connected to the other side of the first guide pipe in a tubular shape larger in diameter than the first guide pipe, and including a second guide pipe through which a reaction solution flows through a gap with the first guide pipe; And a liquid transfer unit configured to transfer the reaction liquid contained in another adjacent reaction tank to the negative pressure space.

As one example, the air inlet pipe is formed in the negative pressure space while forming a clearance with the impeller, the through-holes are formed on both sides so that the rotating shaft of the drive motor passes, and communicates with the negative pressure space through one or more openings selected. It is characterized in that it further comprises;

As an example, the fume barrel is characterized in that a plurality of grinding holes are formed on one side facing the impeller.

As an example, the second guide pipe may include a plurality of supports installed on an inner circumferential surface of which a part of the other side of the first guide pipe is accommodated and faces an outer circumferential edge of the first guide pipe. It is fixed to the guide tube, it is characterized in that the diameter of one end toward the first guide pipe connected to form a large expansion region in the gap with the first guide pipe.

As an example, the scum inlet and the scum inlet connected to the buoyancy sphere, the scum inlet which is connected to the buoyancy sphere and exposed to the water flows into the surface and the scum inlet and the negative pressure space are connected to each other. Characterized in that it further comprises; scum removal unit including a tube.

As an example, a chemical liquid inlet including a chemical liquid inlet through which the chemical liquid flows from the outside, and a chemical liquid connection pipe connecting the chemical liquid inlet to the negative pressure space.

As an example, the chemical liquid injection portion, a cone-shaped dispersion weight is mounted in the inner space of the chemical liquid connection tube and at least two spiral grooves or protrusions formed along the outer periphery from the center of the top hitting and dispersing the injected chemical liquid And an induction groove which is formed spirally along the inner circumference of the chemical connection pipe located below the dispersion weight.

On the other hand, the water treatment method using an internal circulation type continuous batch reactor equipped with a liquid transfer stirring device having a scum removal and chemical liquid dispersing function of the present invention, (a) the raw water is introduced into the total anaerobic tank to operate in anaerobic state to release phosphorus Inducing and simultaneously removing organics; (b) transferring the reaction solution of the entire anaerobic tank to the SBR reactor while stirring the SBR reactor using the liquid transfer stirring device according to any one of claims 1 to 7 during the step (a); (c) inducing denitrification and dephosphorization by repeatedly operating the SBR reactor into which the reaction solution of the entire anaerobic tank is introduced in an aerobic state and anaerobic state, and using the liquid transfer stirring device to react the reaction solution of the SBR reactor. Returning to the total anaerobic tank; And (d) precipitating the reaction solution of the SBR reactor after the end of the denitrification and dephosphorization reaction to discharge the supernatant.

As an example, the step (c) is a step of injecting the reaction solution of the entire anaerobic tank into the SBR reactor at each anaerobic time period in the anaerobic time to supply a carbon source for the denitrification of the SBR reactor, the SBR reactor containing nitrate nitrogen And returning the reaction solution to the total anaerobic tank to induce denitrification in the entire anaerobic tank.

As described above, the water transfer method having a scum removal and chemical liquid dispensing function of the present invention, and a water treatment method using an internal circulation type continuous batch reaction device having the same, utilizes negative pressure generated during liquid transfer and agitation. Because it can be collected and removed, there is no need for separate power or equipment to collect and remove scum, which can reduce operating costs and facility maintenance costs.

In addition, by using the negative pressure generated during the liquid transfer and agitation process, the chemical liquid can be introduced into the reaction tank.In addition, the chemical liquid can be rapidly introduced into the reaction tank while colliding and dispersing the flocculation chemical liquid through the dispersion weight installed in the chemical liquid connection tube. After stirring, the mixture is introduced into the reactor to induce complete bonding of the agglomerated chemical in the reactor, resulting in the effect of improving the water treatment efficiency of the reactor.

BRIEF DESCRIPTION OF THE DRAWINGS The side view which shows the structure of the liquid conveyance stirring apparatus which has a scum removal and chemical-liquid dispersion | dispensing function of this invention.
Figure 2a is an exploded view showing the configuration of a liquid transfer stirring device having a scum removal and chemical liquid dispersion injection function according to an embodiment of the present invention.
Figure 2b is a side cross-sectional view showing the configuration of a liquid transfer stirring device having a scum removal and chemical liquid dispersion injection function according to an embodiment of the present invention.
3 is a view showing the configuration of a fume container according to an embodiment of the present invention.
Figure 4a is a view showing the configuration of the liquid transfer unit according to an embodiment of the present invention.
Figure 4b is a view showing the configuration of the liquid transfer unit according to another embodiment of the present invention.
Figures 5a and 5b is a side view showing the configuration of the scum removing unit according to an embodiment of the present invention.
Figure 6 is a side view showing the configuration of the chemical liquid injection unit according to an embodiment of the present invention.
Figure 7 is a side view showing the configuration of the chemical liquid connection tube according to an embodiment of the present invention.
8 is a side view showing an example in which the scum removing unit and the chemical liquid injection unit is connected in parallel according to an embodiment of the present invention.
9 is a view showing an internal circulation type continuous batch reactor having a liquid transfer stirring device having a scum removal and chemical liquid dispensing function of the present invention.

In describing the present invention, the term or word used in the present specification and claims is based on the principle that the inventor can appropriately define the concept of the term in order to best describe the invention of his or her own. It should be interpreted as meanings and concepts corresponding to the technical idea of

1 is a side view showing the configuration of a liquid transfer stirring device having a scum removing and chemical liquid dispensing input function of the present invention, Figure 2a is a liquid transfer stirring apparatus having a scum removing and chemical liquid dispersing input function according to an embodiment of the present invention Figure 2b is an exploded view showing the configuration of, Figure 2b is a side cross-sectional view showing the configuration of a liquid transfer stirring apparatus having a scum removal and chemical liquid dispersion injection function according to an embodiment of the present invention. And Figure 3 is a view showing the configuration of the fume tube according to an embodiment of the present invention, Figure 4a is a view showing the configuration of the liquid transfer unit according to an embodiment of the present invention, Figure 4b is another embodiment of the present invention 5A and 5B are side views illustrating a structure of a scum removing unit according to an exemplary embodiment of the present invention.

In addition, Figure 6 is a side view showing the configuration of the chemical liquid injection unit according to an embodiment of the present invention, Figure 7 is a side view showing the configuration of the chemical liquid connection tube according to an embodiment of the present invention, Figure 8 is an embodiment of the present invention It is a side view which shows the example in which the scum removal part and the chemical | medical solution injection part connected in parallel.

The liquid transfer stirring apparatus (hereinafter referred to as the 'liquid transfer stirring apparatus 3') having the scum removing function and the chemical liquid dispensing function of the present invention may be applied to one or more reaction tanks 1 and 2 selected from two or more reaction tanks 1 and 2. It is installed to transfer the reaction liquid of another adjacent reaction tank, by using the negative pressure generated in this process to remove the scum existing on the water surface of the reaction tank (1, 2) or to disperse the flocculation chemicals introduced from the outside.

1 and 2, the liquid transfer stirring apparatus 3 of the present invention includes a drive motor 10, an impeller 20, a negative pressure space 30, a first guide part 50, and a second guide part ( 60) and the liquid conveyance part 70 is comprised.

The driving motor 10 is to impart a rotational force and may select a suitable one among known motors, and may be driven by a control signal input from an external controller although not shown in the drawing.

One side of the drive motor 10 is provided with a rotating shaft 100 for transmitting the applied rotational force to the impeller 20.

The impeller 20 is connected to the rotary shaft 100 of the drive motor 10 to rotate.

In addition, the impeller 20 is accommodated in the first guide pipe 500 of the first guide part 50 to be described below, and the other reaction tank adjacent to the reaction liquid (hereinafter referred to as 'inner liquid') of the reaction tank 1 By forming a water vortex with respect to the reaction liquid (henceforth "external liquid") conveyed from (2), stirring between reaction liquids and discharge of the stirred reaction liquid are performed.

The negative pressure space 30 is formed between the impeller 20 and the driving motor 10 in a space opposite to a space where water vortex is generated by the impeller 20, and is rotated by the impeller 20. As the stirred reaction liquid is discharged, a negative pressure corresponding thereto is generated, and suction force according to the negative pressure acts in this space.

The negative pressure space 30 is the liquid transfer pipe 70 is connected, the suction force to act to transfer the external liquid of the other reaction tank (2) from the liquid transfer pipe 70, bar for liquid transfer This eliminates the need for a pump, reducing the cost of operating the plant.

In addition, the negative pressure space 30 is selectively connected to any one of the scum removing unit 80 or the chemical liquid injection unit 90 described below, and the collected scum or the injected chemical liquid separately through the negative pressure described above is the reaction tank ( It can be agitated and discharged together with the internal liquid of 1).

The first guide part 50 has a tubular shape and is provided at one side of the first guide pipe 500 accommodating the impeller 20 therein and the first guide pipe 500 facing the negative pressure space 30. It is configured to include a plurality of connecting rods 510 which are spaced apart along the circumferential direction and connected to the driving motor 10, and openings 520 formed by a space between the connecting rods 510.

In this case, the connecting rod 510 may be connected to one side of the driving motor 10 in which the rotation shaft 100 is positioned while forming a downward slope in the outer circumference of the first guide tube 500 in a bar shape.

The opening 520 having an upward inclination gradient is formed by the shape of the connecting table 510, and thus the negative pressure space 30 is multi-directionally exposed in the reaction tank 1, thereby allowing the liquid transfer part. Not only the external liquid of the other reaction tank 2 may be introduced through the 70, but also the scum or the injected chemical liquid and the internal liquid collected in the corresponding reaction tank 1 may be simultaneously or selectively made.

The second guide part 60 is configured to include a second guide pipe 600 connected to the other side of the first guide pipe 500 in a tubular shape larger in diameter than the first guide pipe 500. .

The second guide tube 600 is installed to accommodate a portion of the other side of the first guide tube 500 therein, a plurality of support on the inner circumferential edge facing the outer circumferential edge of the first guide tube 500 610 may be installed and fixed to the first guide tube 500.

At this time, the second guide tube 600 is formed to have a larger diameter of one end toward the first guide tube 500 connected to form an expansion region in the gap with the first guide tube 500.

In such an extended area, a negative pressure is formed in a process in which the reaction liquid is discharged through the first guide pipe 500. The induced fluid is induced while inducing the inflow of the internal fluid from the corresponding reaction tank 1 through the extended area. By allowing the reaction liquid discharged from the first guide tube 500 to be joined and stirred, the stirring performance may be further improved.

The liquid transfer part 70 allows the external liquid contained in another adjacent reaction tank 2 to be transferred to the negative pressure space 30 through the opening 520.

As shown in FIG. 4A, the liquid transfer unit 70 includes a transfer pipe 700 through which the external liquid is transferred from another adjacent reaction tank 2, an accommodation hopper 710 for receiving the transferred external liquid, and one or more selected openings. It may be configured to include an inlet hopper 720 connected to the 520 to allow the external liquid contained in the receiving hopper 710 to be introduced into the first guide pipe (500).

As another example, the liquid transfer part 70 has a curved cross section so as to surround a lower portion of the first guide pipe 500 as shown in FIG. 4B, and one side communicates with the accommodation hopper 710 and the other side. By further including an expansion hopper 730 in communication with the expansion region formed in the gap between the first guide pipe 500 and the second guide pipe 600, in a plurality of places where the negative pressure acts while providing a stable support structure The liquid transfer and inflow of the external liquid are respectively performed so that a more efficient liquid transfer process can be performed.

Hereinafter, with reference to FIG. 2B, the liquid conveyance and stirring operation state of the liquid conveyance stirring apparatus 3 of this invention is demonstrated.

When the anaerobic reaction of the reaction tank 1 and the stirring of the reaction solution are required, the driving motor 10 is operated to agitate the internal liquid contained in the reaction tank 1.

That is, when the impeller 20 receiving the rotational force is rotated according to the operation of the driving motor 10, the internal fluid is firstly guided through the opening 520 of the first guide part 50. Water flowing into the pipe 500 is induced water vortex for the internal liquid.

In the above process, since the negative pressure is generated in the negative pressure space 30 positioned at the rear end of the impeller 20 and the suction force corresponding to the negative pressure is acted upon, the liquid transfer part 70 connected to the negative pressure space 30 is adjacent. The external liquid of the other reaction tank 2 is transferred and introduced into the negative pressure space 30.

Thereafter, the water vortex acting on the first guide tube 500 according to the rotational driving of the impeller 20 stirs the external liquid introduced from the other reaction tank 2 adjacent to the internal liquid of the reaction tank 1, It is discharged to the reaction tank 1 through the second guide tube 600 by the immediateness is to perform the stirring and the liquid transfer of the reaction solution.

In addition, during the stirring and the liquid transfer process, as described above, in addition to the negative pressure space 30, negative pressure is generated in the expansion region formed in the gap between the first guide pipe 500 and the second guide pipe 600. Bar, the inner liquid of the reaction tank (1) also flows through the expansion zone to be stirred and discharged together with the inner liquid and the outer liquid to make the stirring process more effective.

Although not shown in the drawings, the reaction liquid of the stirred and discharged reaction tank 1 may be conveyed to another adjacent reaction tank 2 through a conveying pipe. Here, the transfer and conveyance between the two reaction tanks (1, 2) may be made before and after at intervals of time, but it is natural that the mutual circulation may be made at the same time as the time set for the transfer and conveyed amount.

Usually, in order to agitate the internal liquid during the anaerobic reaction of the reaction tank (1), a stirring device must be provided, and in order to transfer the external liquid in the adjacent other reaction tank (2) to the reaction tank (1), the present invention The liquid transfer stirrer 3 of the apparatus does not need to install separate equipment for agitation and liquid transfer between the two reaction tanks 1 and 2 by performing the liquid transfer at the same time by using a negative pressure, and thus the equipment including the power cost. The operating cost can be reduced.

Meanwhile, the liquid transfer stirring apparatus 3 according to an embodiment of the present invention may further include a fume container 40 installed in the negative pressure space 30 as shown in FIG. 3.

The fume cylinder 40 may be installed in the negative pressure space 30 while forming a gap with the impeller 20, and each of the through holes 400 may be provided at both sides thereof so that the rotation shaft 100 of the driving motor 10 passes. Formed.

In addition, the fume container 40 is provided with an air inlet pipe 410 for communicating with the negative pressure space 30 through one or more selected openings 520 and receiving external air.

That is, the fume container 40 forms another space which is affected by the negative pressure in the negative pressure space 30, while allowing air to be introduced from the outside through the air inlet pipe 410 under the action of negative pressure. The aeration is caused by dissolving in the reaction liquid through the water vortex generated by the impeller 20.

In particular, the fume container 40 is formed with a plurality of grinding holes 420 on one side facing the impeller 20, the grinding hole 420 is a fine aeration by finely grinding the particles of air supplied from the outside It can be derived.

The fume container 40 can be applied during the aerobic reaction of the reaction tank 1, it is preferable to be configured in a structure that can be selectively detachable in accordance with the aerobic or anaerobic treatment process of the reaction tank (1).

In addition, the liquid transfer stirrer 3 of the present invention is a manual operation method in which the user selects the agitation or aeration action according to the waste and waste water conditions during the aerobic reaction to generate aeration and the BOD (Biochemical Oxygen) of the reaction solution contained in the reaction tank. It is configured to form an automatic measuring circuit and a known measuring sensor for measuring the demand value, MLSS (Mixed Liquor Suspended Solids) value, etc. Can be.

Meanwhile, the liquid transfer stirring apparatus 3 of the present invention collects and removes scum present in the reaction tank 1 by using the negative pressure acting in the negative pressure space 30 as described above, or injects the coagulated chemical liquid into a separate power source. It can be done without.

Specifically, the liquid transfer stirring apparatus 3 of the present invention may further include a scum removing unit 80 and a chemical liquid injection unit 90.

First, the scum removing unit 80 is connected to the buoyancy sphere 800 and the buoyancy sphere 800, which is elevated according to the level of the reactor 1, as shown in FIG. A scum inlet 810 into which the scum is introduced may be included, and a scum connecting tube 820 connecting the scum inlet 810 and the negative pressure space 30 to each other.

The scum inlet 810 may suck and collect scum existing on the water surface by suction force according to the negative pressure of the negative pressure space 30, and the collected scum is collected through the scum connection pipe 820. It flows into the space 30.

Then, the scum introduced into the negative pressure space 30 is pulverized into fine particles by the impeller 20, and then the water inside the reaction tank 1 by the water vortex action of the impeller 20 and the outside of the adjacent other reaction tank 2. It can be decomposed during the anaerobic reaction of the reaction tank 1 by being discharged while stirring with the liquid.

Wherein the scum connection pipe 820 may be applied to a variety of pipes according to the known technology, it is preferable that the tube is configured to be fluidly interlocked to the buoyancy ball 800 to be elevated according to the water level, straight pipe 820-1 In the case of applying), as shown in FIG. 5B, the pipe is connected through a rotary joint pipe 821-1, which enables rotation between the pipe and the pipe.

Meanwhile, as shown in FIG. 6, the chemical liquid inlet 90 is a chemical liquid inlet 900 through which the chemical liquid is introduced from the outside, and a chemical liquid connector 910 interconnecting the chemical liquid inlet 900 and the negative pressure space 30. ) May be included.

Like the scum removing unit 80, the chemical liquid input unit 90 also introduces the agglomerated chemical liquid supplied from the outside into the negative pressure space 30 through suction force by the negative pressure of the negative pressure space 30, and the impeller It can be stirred together by 20 to be discharged to the reaction tank (1).

In this case, the chemical liquid injection unit 900 is configured such that the chemical liquid inlet 900 and the chemical liquid connection tube 910 are located in the water so that the chemical liquid inlet 900 and the liquid may be introduced and transported together with the internal liquid of the reaction tank 1 during the inflow of the agglomerated chemical liquid. Do.

And, referring to Figure 7, the chemical liquid injection portion 90 is mounted in the inner space of the chemical liquid connection pipe 910 in a conical shape and spiral grooves 921-1 or projections 921 along the outer periphery from the center of the top -2) further comprises at least two dispersion weights 920 and at least two guide grooves 930 are formed spirally along the inner circumference of the chemical connection pipe 910 located below from the dispersion weight 920, Can be configured.

That is, the coagulated chemical solution injected into the chemical connection pipe 910 hits the upper end of the cone to be dispersed by the first blow, and then the dispersed chemical solution is formed in a spiral along the outer circumference of the dispersion weight 910 ( 921-1) or to be radially distributed along the protrusion 921-2.

In this way, the dispersion-induced chemical liquid is quickly moved so as not to stagnate along the spiral guide groove 930 formed at a predetermined interval on the inner circumference of the chemical liquid connection pipe 910 and the reaction liquid of the dispersed chemical liquid and the introduced reaction tank 1 is It can be transferred to the negative pressure space 30 in a rapid stirred state.

According to an embodiment of the present invention, the scum connecting pipe 820 or the chemical liquid connecting pipe 910 specifies an example in which the negative pressure space 30 is connected to the negative pressure space 30, but the present invention is The present invention is not limited thereto, and in addition to the negative pressure space 30, it is natural that the apparatus can communicate with various points at which negative pressure is generated.

For example, the scum connecting tube 820 or the chemical liquid connecting tube 910 is an extension region formed in the gap between the first guide tube 500 and the second guide tube 600, or the liquid transfer part 70 If the location is affected by negative pressure, etc., it can be connected anywhere.

In addition, the liquid transfer stirring apparatus 3 of the present invention, as described above, but the scum removing unit 80 and the chemical liquid injection unit 90 is shown an example each independently installed, but the present invention is not limited to this, Fig. As shown in 8, the bottom of the scum connection pipe 820 and the chemical liquid connection pipe 910 are connected in parallel to each other, and the three-way valve 100 for controlling the flow of fluid is mounted on the connection site to thereby control external signals. Of course, it is possible to selectively perform the scum removal process or the input of the chemical solution through.

Liquid transfer stirring device (hereinafter referred to as 'liquid transfer stirring device') having a scum removal and chemical liquid dispensing function of the present invention is installed in at least one reaction tank (1, 2) selected from two or more reaction tanks (1, 2) adjacent to The reaction solution of the other reactor is transferred, and scum present on the water surface of the reactors 1 and 2 is removed by using the negative pressure generated in this process, or the coagulated chemical liquid introduced from the outside is dispersed and added.

9 is a view showing an internal circulation type continuous batch reactor having a liquid transfer stirring device having a scum removal and chemical liquid dispensing function of the present invention.

Referring to Figure 9, the water treatment method (hereinafter referred to as 'water treatment method') using the internal circulation type continuous batch reactor equipped with a liquid transfer stirring device having a scum removal and chemical liquid dispensing function of the present invention is an internal circulation type continuous It can be implemented by a batch reactor.

The internal circulation continuous batch reactor consists of two reactors.

Here, the two reaction tanks may be a pre-anaerobic tank (1) and an SBR reaction tank (2), and each of the pre-anaerobic tank (1) and the SBR reaction tank (2) is provided with the liquid transfer stirring device (3). The circulation of the material between 2) is configured through the liquid transfer stirring device (3).

That is, the entire anaerobic tank 1 spatially divides and shares the reaction to be made in the SBR reaction tank 2 in which the continuous batch reaction process takes place, and according to the change in the concentration of organic matter and the flow rate of the influent raw water, It is configured to maximize the treatment efficiency of nitrogen and phosphorus by adjusting the circulation and frequency.

As used herein, the term 'raw water' refers to all sewage, sewage, and wastewater that is processed and flowed into an internal circulation type continuous reactor, and the term 'reaction liquid' is introduced into an entire anaerobic tank or an SBR reactor. Means any sewage or wastewater that is stored in a tank or where biological reactions occur and that travel between tanks.

On the other hand, the pre-aerobic tank (1) is preferably composed of about 30% of the total volume of the tank, SBR reaction tank (2) of about 70% of the total volume of the tank, in the pre-aerobic tank (1) undergoing anaerobic reaction with the incoming raw water The reaction liquid is transferred to the SBR reaction tank 2 by the liquid transfer stirring device 3, and contains an SBR reaction tank containing nitric acid nitrogen (NO3-N) generated through an aerobic reaction in the SBR reaction tank 2 (2). The reaction liquid in) is returned to the total anaerobic tank 1 through the liquid transfer stirrer 3 provided in the total anaerobic tank 1.

In the present invention, the inlet water is introduced into the total anaerobic tank (1) along the inlet pipe (4), the intermittent or continuous injection is made depending on the organic matter concentration of the inlet water from the pre-anaerobic tank (1) to the SBR reaction tank (2).

And the supernatant is finally treated in the SBR reactor 2 is discharged intermittently along the supernatant discharge device 5 and the supernatant discharge pipe (6).

On the other hand, the excess sludge produced in the microbial reaction process is drawn to the excess sludge discharge device (7) installed in the SBR reactor (2) and transported to the outside to brew without increasing the concentration of microorganisms in the total anaerobic tank (1) and SBR reaction tank (2) Ensure that a certain level of microbial concentration as required by (1, 2) is maintained.

The reaction liquid in the total anaerobic tank 1 is injected into the SBR reactor 2 at the anaerobic reaction time of the SBR reactor 2 by the liquid transfer stirring device 3 provided in the SBR reactor 2, and the SBR reactor ( The reaction liquid of 2) is returned to the total anaerobic tank 1 through the liquid transfer stirring device 3 provided in the total anaerobic tank 1.

At this time, scum that may occur in the anaerobic reaction of the entire anaerobic tank (1), nutrient solution that can be used during the reaction of the SBR reaction tank (2), etc. are selectively removed or removed using the negative pressure of the liquid transfer stirring device (3) installed in each tank Can be committed.

In addition, the same liquid transfer stirring device 3 is installed in the entire anaerobic tank 1 and the SBR reaction tank 2 so that mutual liquid transfer is performed through the liquid transfer stirring device 3 so that it occurs in each tank (1, 2). It is possible to offset the pressure to be made, there is an effect that the amount of agitation can be increased according to the pressure offset.

Here, the injection / conveying between the brews 1 and 2 may be made before and after the time interval, and the mutual circulation may be simultaneously performed by a predetermined time.

In order to agitate the internal liquid during the anaerobic reaction of the SBR reaction tank (2), a stirring device must be provided, and in order to transfer the reaction liquid in the entire anaerobic tank (1) to the SBR reaction tank (2), The liquid transfer stirring device 3 of the present invention can transfer the reaction liquid of the entire anaerobic tank 1 to the SBR reaction tank at the same time as stirring, as described above, so that a separate pump does not need to be installed, thereby reducing the pump operating power cost. Can be.

Detailed configuration of the liquid transfer stirring device 3 has been described above in detail, and thus description thereof will be omitted.

Hereinafter, the functions of the whole anaerobic tank 1 and the SBR reactor 2 of the internal circulation type continuous batch reactor presented in one embodiment of the present invention will be described in more detail.

The SBR reactor 2 is composed of one operation cycle that is converted into anaerobic (inflow) / exhalation / anaerobic (inflow) / exhalation / ... / anaerobic / exhalation / sedimentation / discharge form over time, Nitrogen is denitrified in the anaerobic state and finally removed with nitrogen gas (N 2).

However, organic matter in the reaction solution is not only removed in anaerobic state but also in aerobic state irrelevant to the final removal of nitrogen. Therefore, in order to increase the nitrogen removal efficiency, almost no organic matter is removed when the SBR reactor 2 is in an aerobic state, and almost all amounts of organic matter are preferentially used and removed in the anaerobic state where denitrification occurs.

In order to achieve this purpose, the reaction solution in the anaerobic time zone of the SBR reactor (2) causes a step feed from the entire anaerobic tank (1) to the SBR reactor (2), so that the required carbon source (organic matter) in the SBR reactor (2) By appropriately supplying), it is possible to solve the problem of lack of carbon source in the general sewage treatment process and to obtain stable treatment efficiency.

On the other hand, when the concentration of influent organic matter is increased, such as the area where the sewage sewer pipe is installed, the reaction liquid may be introduced into the SBR reactor 2 not only in the anaerobic time but also in the aerobic time so that the removal of organic matter occurs in the aerobic time.

However, depending on the size of the influent organic matter, the amount of inflow into the aerobic period should be adjusted.

The reason why the pre-anaerobic tank (1) was placed at the front end of the SBR reactor (2) was to promote the hydrolysis of organic matter in the initial influent water by anaerobic reaction in the pre-anaerobic tank (1) to improve the effect of phosphorus release and at the same time This is to remove nitrogen by denitrifying (N2) NO3 -N contained in the return water transferred from (2) to the total anaerobic tank (1).

Since the removal of NO 3 -N in the total anaerobic tank (1) lowers the NO 3 -N concentration of the SBR reactor (2) to prevent the decrease in phosphorus removal rate by the influence of NO 3 -N in the SBR reactor (2). Can be.

In anaerobic conditions, phosphorus release should occur, but in the presence of NO3 -N, microorganisms use NO3 -N as the final electron acceptor, causing phosphorus intake rather than phosphorus release. In addition, since Pseudomonas and Acinetobacter have high phosphorus removal rate, there is competition in terms of substrate intake. Is promoted, and the growth of Acinetobacter is reduced.

At this time, in order to maximize the removal rate of phosphorus Acinetobacter rather than Pseudomonas (Acinetobacter) should be the dominant species in the SBR reactor (2).

Therefore, the SBR reactor 2 located at the rear end of the pre-anaerobic tank 1 removes organic matter and nitrogen by denitrification reaction using organic matter in the influent water as a carbon source in the anaerobic state, and release of phosphorus occurs. In addition, in the aerobic state of the SBR reaction tank (2) there is no inflow of influent, so that the removal and residual nitrification of the organic matter in the tank takes place and the absorption of phosphorus occurs.

The lower the concentration of organic matter in the aerobic state of the SBR reactor (2) is the dominant rate of nitrifying microorganism increases.

In addition, since the anaerobic / aerobic state of the SBR reactor 2 changes repeatedly over time, Acinetobacter, which is relatively more proliferative than other microorganisms, becomes a dominant species, thereby increasing phosphorus removal rate.

Phosphorus is finally removed by removing these microorganisms with a high phosphorus removal rate with sludge immediately after the end stage aerobic reaction or treated water discharge time of the SBR reactor (2) where phosphorus absorption occurred.

On the other hand, the reaction from the entire anaerobic tank (1) to the SBR reactor (2) in order to increase the removal efficiency of contaminants during the last operation mode (expiration / sedimentation / discharge) performed in one cycle of the operation of the SBR reactor (2). The inflow or return of the liquid is prevented from occurring, and during this period, the raw water continuously introduced into the total anaerobic tank 1 is temporarily stored in the total anaerobic tank 1. Therefore, the partial space of the total anaerobic tank 1 located at the front end of the SBR reaction tank 2 also serves as a flow adjusting tank.

[Table 1] below focuses on aspects of operation of the reactor of the SBR reactor (2) in terms of the stage inflow from the entire anaerobic tank (1) to the SBR reactor (2) and the return from the SBR reactor (2) to the total anaerobic tank (1). As shown.

-Basic setting of operation type (1 Cycle) of SBR reactor- division Reaction Sequence of SBR Reactor with Time Anaerobic 1 (inflow) Exhalation 1 Anaerobic 2 Unit 2 Anaerobic 3 Unit 3 Sedimentation exhaust Step inflow and
Cycle □ □ □ Inflow and circulation (about 60%) Inflow and circulation (about 35%) Inflow (about 5%) [Note] 1. The stage inflow and circulation timing refers to the introduction of the reaction solution from the entire anaerobic tank into the SBR reactor, or the circulation of the reaction liquid back to the entire anaerobic tank. 2. The inflow and circulation rate (%) depends on the pollutant load of the influent. 3. "□" indicates when step inflow and circulation takes place.

The time interval of the operation mode shown in [Table 1] may be set differently as in the example of [Table 2] below according to the change in the contaminant concentration and the inflow of the influent.

-Example of operating method of SBR reactor according to inflow and pollutant concentration 1 minute in cycle Operation Method of SBR Reactor Remarks Anaerobic 1 Exhalation 1 Anaerobic 2 Unit 2 Anaerobic 3 Unit 3 Sedimentation exhaust 360 50 50 50 50 50 50 40 20 360 45 50 45 50 45 50 55 20 300 40 40 40 40 40 40 40 20 240 30 30 30 30 30 30 40 20 210 Exhalation only 150 minutes (continuous circulation of the entire anaerobic tank and SBR reactor) 40 20 180 Exhalation only 150 minutes (continuous circulation of the entire anaerobic tank and SBR reactor) 40 20

As shown in Table 2, the SBR reactor 2 can be operated by various operating methods according to the inflow flow rate and the contaminant concentration change. For example, when a processing time per cycle is 4 hours or more, the operation method described in Table 1 is operated.

When the flow rate increases, one cycle treatment time is operated at 4 hours or less. At this time, the SBR reactor 2 only has an aerobic reaction as shown in [Table 3] below, and the liquid of the brews (1, 2) is transferred to each liquid. While continuously circulating through the stirring device (3), the entire anaerobic tank (1) is to function as an anoxic tank required for denitrification.

As described above, in the water treatment method of the present invention, the treatment of nitrogen and phosphorus is possible even with a short one-cycle treatment time, so that it is possible to flexibly cope with changes in the amount and quality of the influent, so that the invention is suitable for sewage treatment in Korea.

In addition, in the case of the liquid transfer stirring device (3), a device for smooth material exchange between the breweries (1, 2), in order to increase the anaerobic reaction at the anaerobic time, a stirring device is necessary, and the SBR reaction tank (2) and the whole anaerobic tank The liquid transfer device (pump) is required for the material exchange between (1), but the liquid transfer stirring device (3) of the present invention has the stirring function of the SBR reaction tank (2) and the SBR reaction tank (2) in the total anaerobic tank (1). It is characterized by the fact that the liquid transfer can be carried out simultaneously or independently.

The operation of the liquid transfer stirring device 3 is performed according to the characteristics of the wastewater and the operating conditions of the SBR reactor 2, so that the efficiency of nitrogen and phosphorus removal in the wastewater can be improved.

For example, although not shown in the drawing, a water level meter, a dissolved oxygen meter, an oxidation / reduction potentiometer, a microbial concentration meter, a pH meter are installed in the SBR reactor 2, and a water meter, a dissolved oxygen meter, By installing an oxidation / reduction potentiometer, etc., it is possible to promptly detect and control the change in the operating state and to cope with it flexibly to improve the processing efficiency.

Example 1 Sewage Treatment Using an Internal Circulation Continuous Batch Reactor

In order to verify the effect of the present invention, a small scale experimental apparatus was manufactured and the first field experiment was conducted for about one year. The effective capacity of the total anaerobic tank (1) and the SBR reactor (2) was 0.9m ³ and 1.8m ³ , respectively, and it was operated at 4 cycles per day with a throughput of 0.6m ³ per cycle, so the total daily treatment capacity was 2.4m. ^The internal circulation type continuous batch reactor was configured to be 3.

In addition, after installing water quality measurement sensors and monitoring devices such as pH, DO, water temperature, and ORP in the reactor, each server (C university) and client (J company) that receive, store, and manage the site host and each information are located. The experiment was conducted by establishing a real-time field tester monitoring and control system suitable for the site. The experimental apparatus was installed in the sewage treatment plant at N city, and the reactor operation mode was configured as shown in the following [Table 3].

In the present Example 1, the water level of the total anaerobic tank 1 is as shown in Table 4 below.

-Basic setting of operation type of SBR reactor- 1Cycle Composition of SBR Reactor Reaction time (min) Stage inflow (min) Step return (min) Anaerobic 1 50 23 10 Exhalation 1 50 Anaerobic 2 50 17 5 Unit 2 50 Anaerobic 3 50 10 Unit 3 50 Sedimentation 40 exhaust 20 [Note] 1. 'Stage inflow' refers to the transfer of the reaction solution from the entire anaerobic tank to the SBR reactor. 2. 'Step return' refers to the transfer of the reaction solution from the SBR reactor to the entire anaerobic tank.

-Level change of all anaerobic tanks during stage inflow and stage transfer- 1Cycle Composition of SBR Reactor Stage inflow (min) Step return (min) Water level of the entire anaerobic tank (mm) Anaerobic 1 23 10 1230 Exhalation 1 Anaerobic 2 17 5 1026 Unit 2 Anaerobic 3 10 Unit 3 1480 Sedimentation exhaust 1800 [Note] 1. 'Stage inflow' refers to the transfer of the reaction solution from the entire anaerobic tank to the SBR reactor. 2. 'Step return' refers to the transfer of the reaction solution from the SBR reactor to the entire anaerobic tank.

As shown in [Table 4], the inflow of the inlet for 23, 17, 10 minutes, the level of the total anaerobic tank (1) after the end of the step return 10, 5 minutes was 1,230mm and 1,036mm, the total amount of step conveyance It was operated at the same flow rate as the raw water inflow.

On the other hand, after the reaction, the analysis results of the water treatment in the entire anaerobic tank (1) and the SBR reactor (2) are as shown in [Table 5] below. The removal efficiency of TCOD CR, TN (total nitrogen) and TP (total phosphorus) is 97.7%, 84.8% and 85.4% were very high. Influent and treated water were analyzed for water quality according to the process method (Standard Method, APHA, 1992) 2-4 times a week.

-Analysis of Water Treatment in All Anaerobic and SBR Reactors- division TCODcr (mg / l) T-N (mg / l) NO ₃ -N (mg / l) NH ₃ -N (mg / l) T-P (mg / l) Influent 438.9 61.1 1.7 12.1 7.08 A complete anaerobic tank 81.5 19.2 1.6 9.7 5.48 SBR reactor after stage inflow 20.5 12.0 2.6 2.2 2.85 All anaerobic tanks after step return 53.4 6.4 1.2 7.8 3.12 Runoff 10.3 9.3 3.7 0.3 1.03 efficiency(%) 97.7 84.8 - 97.9 85.4 [Note] 1. 'Stage inflow' refers to the transfer of the reaction solution from the entire anaerobic tank to the SBR reactor. 2. 'Step return' refers to the transfer of the reaction solution from the SBR reactor to the entire anaerobic tank.

Example 2 Sewage Treatment Experiments Using an Internal Circulation Continuous Batch Reactor Equipped with Liquid Transfer Stirring Device of the Present Invention

In order to test the performance of the liquid transfer stirring apparatus 3 as well as the sewage treatment efficiency of the internal circulation type continuous batch reactor, a second field experiment was performed by installing an experimental apparatus 25 times larger than the treatment capacity of Example 1.

That is, the effective capacity of the total anaerobic tank 1 used in the experiment of Example 2 was 18.75 m ³ (width 2.5 m × length 2.5 m × height 3 m), and the effective capacity of the SBR reactor 2 was 37.5 m ³ ( 2.5m wide x 5m long x 3m high), and the treatment capacity per cycle was 15m ³ and operated at 4 cycles per day to produce an internal circulation type continuous batch reactor so that the total treatment capacity per day was 60m ^3. The experiment was performed by placing it next to the experimental apparatus of 1.

As shown in Fig. 9, the internal circulation type batch reactor was constructed and the liquid transfer stirrer having a driving power of 2 hp was installed as shown in Fig. 9, and the entire anaerobic tank (1) flow rate, the SBR reaction tank (2) flow rate, An anaerobic tank (1) installed a flow meter to measure the instantaneous flow and the accumulated flow so as to know the conveyed volume and discharge amount, and a water level meter to measure the water level of the brewing tanks (1, 2) according to the moment. After the integration agometer was installed, the efficiency test and the hydraulic test of the reactor were conducted using the influent of N sewage treatment plant.

Reactor operation and water quality analysis were performed in the same manner as in Example 1, and the treatment efficiency thereof is shown in Table 6 below.

That is, the removal efficiencies of TCODCR, T-N (total nitrogen) and T-P (total phosphorus) were 95.8%, 86.0%, and 85.5%, which were very high as in Example 1.

-Analysis result of water treatment of SBR reactor and total anaerobic tank- division TCODcr (mg / l) T-N (mg / l) NO ₃ -N (mg / l) NH ₃ -N (mg / l) T-P (mg / l) Influent 384.4 35.8 10.5 5.76 Runoff 16.0 5.0 0.0 0.84 efficiency(%) 95.8 86.0 100.0 85.5

In particular, the agitation of the SBR reactor (2) was satisfactory during the operation of the liquid transfer stirring device (3). .

-Liquid transfer amount according to the impeller rotation speed of liquid transfer stirrer Rpm Required power Liquid transfer amount (All anaerobic tank-> SBR reaction tank) Remarks 1750 2 hp 23m ³ / hour 1452 1.6 hp 20m ³ / hour 1150 1.3 horsepower 18m ³ / hour 875 1 horsepower 15m ³ / hour 600 0.6 hp 8m ³ / hour

As shown in [Table 7], the liquid transfer efficiency of the liquid transfer stirring device 3 having a 2 horsepower driving force was 15 m ³ / hour when driven at 1 horsepower. This eliminates the need for a separate pump operation, saving one horsepower (0.75 KW) per hour.

Although the preferred embodiments of the present invention have been described in detail above, the scope of the present invention is not limited thereto, and various modifications and improvements of those skilled in the art using the basic concepts of the present invention defined in the following claims are also provided. It belongs to the scope of rights.

1: All anaerobic tank 2: SBR reactor
3: liquid transfer stirring device of the present invention 4: inlet pipe
5: supernatant drainage system 6: supernatant drainage pipe
7: sludge discharge device 8: aeration device
10: drive motor 20: impeller
30: negative pressure space 40: fume container
50: first guide portion 60: second guide portion
70: liquid transfer unit 80: scum removal unit
90: chemical injection portion 100: rotation axis
400: through hole 410: air inlet pipe
500: first guide pipe 510: connecting rod
520: opening 600: second guide pipe
800: buoyant sphere 810: scum inlet
820: Scum connector 900: chemical liquid inlet
910: chemical liquid connector

Claims (9)

In the apparatus for transferring the reaction liquid of the other adjacent reaction tank is installed in at least one selected from the two or more reaction tank,
A drive motor to impart rotational force;
An impeller connected to the rotating shaft of the driving motor and interlocked with the rotating shaft;
A negative pressure space formed between the impeller and the driving motor, the negative pressure space being generated by the rotation of the impeller;
It is formed by a plurality of connecting rods and spaced space between the connecting rods installed in the circumferential direction on one side of the first guide tube for receiving the impeller in a tubular shape and the first guide tube facing the negative pressure space and connected to the drive motor. A first guide part including an opening portion;
A second guide part connected to the other side of the first guide pipe in a tubular shape larger in diameter than the first guide pipe, and including a second guide pipe through which a reaction solution flows through a gap with the first guide pipe;
A liquid transfer unit configured to transfer the reaction liquid contained in another adjacent reaction tank to the negative pressure space; And
It includes a chemical liquid inlet through which the chemical liquid is introduced from the outside and the chemical liquid inlet tube and the negative pressure space interconnection, wherein the chemical liquid inlet and the chemical liquid connection tube is configured in the underwater position in the reaction tank, mounted in the negative pressure space And a chemical liquid inlet unit which is agitated together by the impeller while being discharged from the chemical liquid inlet through the suction force by the negative pressure of the negative pressure space into the negative pressure space and discharged to the reaction tank.
The chemical liquid injection unit,
Conical shape is mounted on the upper portion of the inner space of the chemical liquid connection tube and at least two spiral grooves or protrusions are formed along the outer periphery from the center of the upper end, and the chemical liquid injected into the chemical liquid connection tube hits the upper end of the cone and blows primarily. Spiral along the inner periphery of the dispersing weight and the lower portion of the chemical liquid connecting tube located below the dispersing weight to induce the radial dispersion of the dispersed liquid along the grooves or protrusions are formed spirally while the dispersion by Formed to form a liquid transport with a chemical liquid dispersion input function, characterized in that it further comprises an induction groove to be transferred to the negative pressure space in a state in which the chemical liquid induced in the dispersion in the dispersion weight and the reaction liquid flowing from the reaction tank rapidly stirred state Stirring device.
The method of claim 1,
A fume barrel installed in the negative pressure space while forming a clearance with the impeller, and having a through hole formed at both sides thereof so that the rotation shaft of the driving motor passes therethrough, and an air inlet pipe communicating with the negative pressure space through one or more selected openings; Liquid transfer stirring device having a chemical liquid dispersion injection function, characterized in that it further comprises.
The method of claim 2,
The fume container,
A liquid transfer stirring apparatus having a chemical liquid dispersion input function, characterized in that a plurality of grinding holes are formed on one side facing the impeller.
The method of claim 1,
The second guide tube,
A part of the other side of the first guide tube is accommodated therein, and a plurality of supports are installed on an inner circumference facing the outer circumference of the first guide tube to be fixedly connected to the first guide tube and connected to the first guide. A liquid transfer stirring apparatus having a chemical liquid dispensing injection function, characterized in that the diameter of one end toward the tube is large to form an expansion region in the gap with the first guide tube.
The method of claim 1,
A scum inlet which rises and lowers according to the level of the reactor, a scum inlet connected to the buoyancy sphere to expose the surface of the scum that is present on the surface, and a scum connecting tube which interconnects the scum inlet and the negative pressure space to each other; Liquid removal stirring device having a chemical liquid dispersion input function, characterized in that it further comprises a com-Remover.
delete delete (a) introducing raw water into the total anaerobic tank to drive anaerobic to induce the release of phosphorus and at the same time to remove organic matter;
(b) transferring the reaction solution of the entire anaerobic tank to the SBR reactor while stirring the SBR reactor using the liquid transfer stirrer according to any one of claims 1 to 5 during the step (a);
(c) inducing denitrification and dephosphorization by repeatedly operating the SBR reactor into which the reaction solution of the entire anaerobic tank is introduced in an aerobic state and anaerobic state, and using the liquid transfer stirring device to react the reaction solution of the SBR reactor. Returning to the total anaerobic tank; And
(d) precipitating the reaction solution of the SBR reactor after the end of the denitrification and dephosphorization reaction, and then discharging the supernatant; a continuous batch reaction device having a liquid transfer stirring device having a function of dispersing the chemical liquid. Water treatment method using.
The method of claim 8,
In step (c),
In the anaerobic time, the reaction solution of the entire anaerobic tank is injected into the SBR reactor every anaerobic time period to supply a carbon source for the denitrification of the SBR reactor, and the reaction solution of the SBR reaction tank containing the nitrate nitrogen is returned to the entire anaerobic tank. Inducing a denitrification reaction in the; Water treatment method using a continuous batch reactor with a liquid transfer stirring device having a chemical liquid dispersion input function comprising a.

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