KR100862184B1 - Anaerobic or anoxic reactor employing density-controlled medias, apparatus and method for treating wastewater using the same - Google Patents

Abstract

The present invention relates to a biological anaerobic / anoxic reaction tank, a wastewater treatment apparatus and a wastewater treatment method using the same, a liquid distribution pipe for distributing the influent wastewater in the reaction tank, the treatment of the inlet air or oxygen-free gas diffuser, gas and carrier treatment By incorporating a treated water separator for separating from water, and adding a carrier whose specific gravity is adjusted to 0.95 or more and less than 1.0 into the reactor, when gas is injected into the reactor, the carrier is fluidized in the reactor and when the gas supply is stopped, We present a method for operating a fixed bed or fluidized bed reactor using the principle of being a floating fixed bed. In addition, in the fixed-bed or fluidized bed reactor, in addition to the wastewater, the after-treatment water, which is lower than the BOD concentration in the reactor, is mixed in excess of two times to lower the concentration of toxic components in the reactor and lower the age of the microbial membrane attached to the carrier surface. We present a breakthrough anaerobic and anaerobic tank design and operation method that maximizes

Biological reactor, anaerobic tank, anaerobic tank, fluidized bed reactor, fixed bed reactor

Description

Anaerobic / Anoxic reactor using controlled carrier with specific gravity, wastewater treatment apparatus and wastewater treatment method using the same {Anaerobic or anoxic reactor employing density-controlled medias, apparatus and method for treating wastewater using the same}

Figure 1 is a block diagram showing an anaerobic / anaerobic reactor according to the present invention.

2 is a cross-sectional view of the treated water separator of the present invention.

<Description of the symbols for the main parts of the drawings>

1: Reactor tank 2: Water surface layer

3: carrier layer 4: liquid distribution tube

5: gas diffuser 6: treated water separator (GLM separator)

7 carrier blocker 8 gas blocker

9: sludge bed 10: anaerobic gas outlet

11: treated water outlet 12: wastewater inflow

13: Treated Water Outflow 15: Anaerobic Gas Recirculation

16: air inflow 17: back-end treated water return

18: gas blower 19: anaerobic gas inlet valve

20: air inlet valve 21: timer

The present invention relates to an anaerobic / anoxic reaction tank, a wastewater treatment apparatus and a wastewater treatment method using the same, and more particularly, the carrier layer is controlled to a fluidized bed or a fixed bed state by injecting or blocking gas through a gas diffuser. It relates to an anaerobic / anoxic reaction tank using a carrier having a specific gravity that can be treated, a wastewater treatment apparatus and a wastewater treatment method using the same.

The biological anaerobic reactor not only has a low energy cost, but also converts the non-degradable wastewater into biodegradable by acid fermentation, converts organic nitrogen into inorganic ammonia by ammonification, and prevents methanogenesis. The COD is lowered and the sludge is reduced a lot, so there are various advantages over the aerobic reaction tank, but it is weaker in toxicity and slower than the aerobic reaction.

On the other hand, organic nitrogen-containing wastewater converted to inorganic ammonia in an anaerobic tank or wastewater containing ammonium ions in the first place is nitrified to nitrate nitrogen in an aerobic tank and then reduced to nitrogen gas through denitrification with hydrocarbon reducing agents such as BOD in raw water. The reactor then takes place under oxygen-free conditions, like anaerobic reactions.

The anaerobic or anoxic tank needs to increase its concentration by accumulating sludge in the reactor to increase the reaction rate and achieve sludge reduction. As seen in a typical UASB (upflow anaerobic sludge blanket) reactor, the sludge accumulates in the lower part by its own gravity sedimentation, or a gas-liquid-solid (GLS) separation unit is installed inside the reactor to accumulate sludge and discharge wastewater into the sludge layer. Preferred is a fixed bed reactor that passes in an upflow.

However, such a fixed bed reactor has a low removal rate at the inlet, the high concentration of highly toxic wastewater has a disadvantage in that the operation of the microorganism is lowered to stabilize the operation. In order to stably treat the highly concentrated and highly toxic wastewater, a mixed reactor that uses a mechanical stirrer, injects nitrogen gas, or internally circulates anaerobic gas and stirs to uniform concentration in the reactor is preferred, but in this case, to accumulate sludge in the reactor There is a disadvantage in that the sludge concentrated in the latter settling tank should be returned into the reactor.

Recently, in order to increase the reaction rate by increasing the amount of microorganisms in the anaerobic tank, a large number of adhesion-grown anaerobic tanks using a solid medium having a high surface area have been introduced. However, one example of such a fluidized-bed mixed reactor is to accumulate sludge by recirculating the carrier from the bottom to the top through an externally mounted pipe in the US Patent Publication No. 2003-0209476 and embedding a disc-shaped solids separator rotating at the top. A complex design approach is introduced. An example of a fixed-bed tubular reactor is a parallel passage reactor (PPR) in which the carriers in the form of corrugated plates arranged vertically are arranged in parallel in the U.S. Patent (Publication No. 2005-0167359), and to further accumulate sludge in the reactor. The lower sludge is returned to the upper side by using a pump to increase the microbial concentration. The AF (anaerobic filter) reactor, which uses a fixed amount of pellet or chip type carrier, which is the most common carrier, is used as a fixed bed in the anaerobic tank. As a result, backwashing should be performed using high pressure washing water and gas (nitrogen or anaerobic gas), but the smaller the carrier size, the easier backwashing. In Korean Patent Publication No. 2006-0124108, a method of installing a large number of valves at the bottom and purging the biofilm in multiple stages using nitrogen is introduced. In another Korean patent (Publication No. 2006-0124195), after dividing the filter bed into upper and lower stages for more efficient backwashing, the wastewater flows into the upstream and downstream streams, and the nitrogen for backwashing is upflowed. A method has been introduced but this is not a solution if the reactor is large.

As described above, the attached growth-type anaerobic reactor using the carrier is difficult to use as a fluidized bed mixed reactor in the presence of the carrier, and it is difficult to accumulate sludge in the reactor, and when used in the form of a fixed bed tubular reactor The backwashing problem is followed and the driving is difficult.

In addition, the tubular reactor using a corrugated plate or the like has a problem in that the surface area of the carrier is small so that the sludge must be circulated by an external pump.

It is an object of the present invention to provide a wastewater treatment apparatus which is optionally operable in a fluidized or fixed bed.

It is a further object of the present invention to provide a biological anaerobic wastewater treatment apparatus which is optionally operable in a fluidized or fixed bed.

It is another object of the present invention to provide a method for treating wastewater optionally with a fluidized or fixed bed.

It is yet another object of the present invention to provide a method for treating biological anaerobic wastewater, optionally treating wastewater in a fluidized or fixed bed.

Still another object of the present invention is to provide an anaerobic wastewater treatment apparatus capable of anaerobic digestion, ammonialation and denitrification.

It is yet another object of the present invention to provide a method for backwashing a carrier in an anaerobic biological wastewater treatment device operating in a stationary bed.

Another object of the present invention is to provide a novel wastewater treatment system for separating anaerobic gas from treated water and a carrier.

Still another object of the present invention is to eliminate the need for external sludge circulation and to convert to a fixed bed tubular reactor or a fluidized bed mixed reactor if necessary, and to backwash the carrier layer even when used as a fixed bed reactor. It is to provide an anaerobic / anaerobic reactor, wastewater treatment apparatus and wastewater treatment method using the same, which can easily process high concentration and high toxicity wastewater with no need for retransmission and easy operation.

In order to achieve the above object, the biological reaction tank of the present invention is formed with a carrier layer consisting of a submerged floating carrier on the surface of the reaction vessel, characterized in that the carrier layer is selectively fluidized.

In the present invention, the carrier has a specific gravity less than that of water so as to have a form that floats under the water. In the practice of the present invention, it is preferable that the specific gravity of the carrier has a specific gravity of 0.95 or more and less than 1.0 so that it can be fixed in a submerged floating form under the water even when the carrier is filled with a constant thickness to form a fixed carrier layer. Do. When the specific gravity of the carrier is low, the upper surface of the carrier layer may be exposed to the surface of the water by buoyancy, thereby lowering the biological treatment capacity. When the specific gravity of the filter medium is high, the carrier may sink in water.

In the present invention, the microorganism is filled in a certain thickness on the surface of the reactor so that the microorganism is present in a sufficient amount, it is preferable to form a carrier layer of the stationary phase when there is no physical agitation.

In the practice of the present invention, the carrier layer has a specific gravity similar to that of water and can be easily fluidized to fill up to 90% by volume in the reactor, preferably considering the amount of sludge layer in the reactor, 80% by volume, more Preferably up to 70% by volume.

In the present invention, the carrier is preferably provided in the form of particles so that sufficient fluidization can occur, and is preferably used in the form of a hollow or wrinkled on the outer surface to form a large outer surface.

In the present invention, the carrier may be fluidized by various stirring devices, and preferably fluidized by an acidic device. The diffuser may use a variety of gases as long as it does not interfere with anaerobic operation. In one embodiment of the invention, the acidifier device may use air when the biological reaction tank to diffuse the back of the carrier when operating in the stationary phase. In a preferred embodiment of the present invention, the acidic device preferably uses anaerobic gas so that the biological reactor can be operated in an anaerobic tank when operating in fluidized bed. In one embodiment of the present invention, the acid diffuser is preferably formed between the carrier layer and the sludge layer.

In the present invention, the carrier layer is intermittently fluidized when backwashing when the biological reactor is operated in a fixed bed, and the carrier layer is fluidized continuously during the reaction when operating in a fluidized bed.

In the present invention, the biological reactor has a built-in separator for separating the gas and the carrier from the discharged treated water. More preferably, the separator is installed to be submerged below the water surface layer.

The present invention in one aspect, the reaction tank; A stationary bed carrier layer consisting of a submerged floating carrier is formed on the surface of the reactor, and the carrier layer can be selectively fluidized; Diffuser device; A liquid distribution tube for introducing and discharging wastewater into the reactor tank; And a treated water separator for separating and discharging the gas and the carrier from the treated water passed through the carrier layer, and comprises a biological anaerobic reactor, which is operated as a fluidized bed or a fixed bed in accordance with the operation of the acidic device.

In the present invention, the treated water separator is preferably installed to be submerged under the surface layer of the water, and formed integrally with the tubular carrier blocking tube formed with a plurality of holes smaller than the carrier size, and the lower portion of the carrier blocking tube. And a gas barrier plate having a '∧' shape, and each of the carrier and the gas is separated from the treated water to discharge only the treated water into the carrier blocking tube.

In the present invention, the acidifier device is installed in the lower portion of the carrier layer is installed to fluidize the carrier during gas injection, the carrier is adjusted to specific gravity of 0.95 or more to less than 1.0 so as to allow the floating floating, and fluidized by the acid And it is preferable that the length of the cross-section is 2-50 mm in size so that the separation by the carrier blocking tube formed in the treated water separator.

In the present invention, the liquid distribution tube is preferably installed in the lower portion of the reaction tank tank when the influent wastewater is evenly dispersed in the reactor when operating in a fixed bed flows through the sludge bed to flow upstream is preferably configured to be made.

In the practice of the present invention, an outlet for discharging the anaerobic gas is formed in the upper portion of the reactor tank, a blower to the gas diffuser device so that some of the anaerobic gas discharged through the outlet can be recycled into the reactor tank. It is preferable to be installed in communication.

In the present invention, water having a low BOD concentration, for example, return water having a low BOD to be returned and processed at a rear end, may be introduced into the reactor tank to dilute wastewater. Although not theoretically limited, when a low BOD return water is introduced, the concentration of BOD in the anaerobic tank and the concentration of microbial toxic components are lowered, while the concentration of microorganisms attached to the carrier is maintained, and the inactivation of microorganisms is increased due to age. This leads to an increase in removal rate. In the present invention, the returned BOD having low BOD to be treated together with the wastewater is preferably used to be conveyed at the front end of the settling tank so as not to increase the treatment capacity of the settling tank.

In the practice of the present invention, the returned water is preferably introduced in an excess of 2 times or more, more preferably 5 times or more, than wastewater introduced to sufficiently increase the removal rate.

In one aspect, the present invention provides a biological wastewater treatment method comprising treating a wastewater in a fixed bed or a fluidized bed using a biological anaerobic tank in which a carrier layer made of a floating floating carrier is formed on the surface of a reactor that can be selectively fluidized. Is done.

In the present invention, the biological anaerobic tank is formed on the surface of the reactor by the buoyancy buoyancy to form a carrier layer forming a layer. The carrier layer maintains a fixed bed form due to the difference in specific gravity with water, and is formed in a form that can be converted into a fluidized bed by physical agitation such as acid or aeration. It is preferable that the specific gravity is adjusted to 0.95 or more and less than 1.0 so that it can be appropriately changed from the fixed bed form to the fluidized bed form by the diffuser, so that it is a submerged floating form under the water.

In the present invention, the determination of the conversion into the fluidized bed and the fixed bed can be determined by various operating conditions such as the concentration of wastewater flowing into the anaerobic tank, the concentration of toxic substances, the treatment rate, the generation of anaerobic gas, and the like. The operating state can be easily changed by operation. Preferably, it is preferable to operate in a fluidized bed when wastewater concentration or toxicity is high.

The present invention in one aspect, the reaction tank; A carrier layer having a specific gravity of 0.95 or more and 1.0 or less composed of a floating floating carrier on the surface of the reactor; An acidic device for selectively fluidizing the carrier layer; A liquid distribution tube for introducing and discharging wastewater into the reactor tank; And a biological anaerobic tank including a treated water separator for separating and discharging the gas and the carrier from the treated water passing through the carrier layer, thereby providing a biological wastewater treatment method for treating wastewater in a fixed bed or a fluidized bed. do.

In the present invention, the biological anaerobic tank is a liquid phase formed at the bottom of the reactor in the state in which the carrier layer forming a stationary phase in the form of a submerged floating on the surface of the reactor, the sludge layer is formed at the bottom of the reactor when the apparatus does not operate Wastewater is introduced into the pipe, and the wastewater uniformly dispersed at the bottom of the reactor rises through the sludge layer and is discharged through the carrier bed in the form of a stationary phase. The solids accumulating in the carrier layer over time are operated to periodically remove intermittent air, fluidize, backwash and remove air.

In the present invention, the biological anaerobic tank is operated in a fluidized bed in which the carrier continuously flows inside the reactor when the aerator is continuously operated. Sludge etc. are flowed together with the carrier, and it is preferable to use a large amount of the carrier in comparison with the stationary phase to increase the treatment rate. Preferably, the amount of carrier used is 70 vol% or more of the reaction volume.

In one preferred embodiment of the present invention, the anaerobic reaction tank operated in a fluidized bed is capable of complete fluidization even when the carrier is charged to near 90% by volume in the reactor by adjusting the specific gravity of the carrier closer to water, and the reaction efficiency is good. It may be configured not to return the sludge to the reactor after concentration.

In another preferred embodiment of the present invention, the anaerobic reactor operated in the fluidized bed is a sludge that is heavier than water, while controlling the carrier density to be at least 0.99 so as to fluidize even a small amount of gas when the amount of sludge is to be reduced instead of the amount of carrier. The sludge can be further concentrated by allowing sedimentation to occur relatively.

In the present invention, while increasing the treatment efficiency, and also having a lower BOD concentration than the wastewater treated with the reactor tank to enable the denitrification reaction in the anaerobic tank, for example, return water returned from the sedimentation tank with the wastewater together with the wastewater It is preferable to process.

In one embodiment of the present invention, the returned water can be conveyed at the front end of the sedimentation tank. In another embodiment of the present invention, the returned water may use an effluent treated in an aerobic tank or an anaerobic tank further connected to the rear end of the anaerobic reactor.

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

As shown in FIG. 1, when the carrier having a specific height is added to a desired volume of a carrier having a specific gravity, the carrier is formed in the form of a self-floating carrier under the water surface layer 2 when there is no stirring. ) Is achieved. In this case, since the carrier layer is a fixed bed, it is possible to operate as a fixed bed reaction tank, and when the mechanical agitation is performed by injecting anaerobic gas containing no air, the carrier is easily fluidized, thereby operating as a fluidized bed reaction tank.

Here, the carrier is present in the form of a self-floating under the water surface layer by adjusting the specific gravity to more than 0.95 and less than 1.0, it is preferable that the length of the cross-section is produced in the size of 2-50mm. In addition, the carrier layer 3 may be formed so as to occupy 2-90% by volume of the tank in some cases when operating the reaction tank.

It is preferable that such a carrier is hollow for high surface area, and inexpensive polymer mono- or multi-component mixtures or polymer-inorganic mixtures are preferred for economical production. It is possible to produce a variety of shapes by extrusion or injection molding using polypropylene, or a material mixed with another polymer or inorganic material having a specific gravity greater than water. When the carrier of this type is introduced into the reactor containing the wastewater, the carrier does not sink to the bottom of the reactor in water, but floats as a fixed layer in the form of self-floating under the water surface layer. Therefore, there is no need for a screen or support for the carrier layer like a general fixed bed, and when gas is injected, it is converted into a fluidized bed that is completely mixed with water in a short time. Using this principle, the present invention intends to propose an anaerobic / anoxic tank design that can operate in a fixed bed or a fluidized bed according to the type of wastewater, and a wastewater treatment method using the reactors.

The following three main facilities are built into the reactor of the present invention, firstly, a liquid distribution pipe 4 for evenly distributing the incoming wastewater at the bottom, and second, a gas acid pipe 5 for dispersing the incoming air or anaerobic gas. And, thirdly, a gas-liquid-media (GLM) separator 6 (hereinafter referred to as a GLM separator) as the treated water separator for separating the gas and the carrier from the treated water flowing out after the treatment. These three devices basically have a small hole in a circular pipe or a square channel, and can be any type, such as straight, two-dimensional, or circular, depending on the structure and size of the reactor. It can be distributed or distributed evenly in the direction.

The GLM separator 6 is a device for blocking the inflow of gas or carrier when the treated wastewater is discharged to the discharge port, is installed at a predetermined position below the water surface, as shown in the cross-sectional view of FIG. With a carrier blocking pipe (7) for blocking outflow together, and a gas barrier plate (8) having an inverted V-shape, ie, a '∧' shape, to block outflowing gas bubbles along with the treated water. It is composed.

In addition, the gas diffuser (6) is located at the bottom of the carrier layer when operating the carrier layer as a fixed bed to inject air or anaerobic gas for backwashing when the carrier layer is blocked by a solid material, it is operated in a fluidized bed mixed reactor In order to fluidize the sludge and the carrier by continuously injecting anaerobic gas, the installation position is located at a height of 7-70% from the bottom of the reactor depending on the type of reaction tank, the fluidization of the carrier and the degree of sludge concentration.

The reactor having such a configuration is capable of treating the waste water by adjusting the carrier layer to a fluidized bed or a fixed bed state as the gas is injected through the gas diffuser 6 or the gas is blocked. In each case controlled by a fixed bed, the principle of operation and the operating principle of wastewater treatment using this reactor will be explained.

First, when used as a fixed bed tubular reactor, the wastewater raw water 12 introduced into the bottom of the reactor equalizes the flow while passing through the liquid distribution pipe 4 and then the lower sludge layer 9 and the upper carrier layer 3 in an upward flow. In turn, the elimination reaction takes place. While passing through the carrier layer, the sludge does not pass but is filtered and accumulates in the carrier layer and the lower part of the reactor. After the reaction, the wastewater is finally discharged out through the treated water outlet 11 through the GLM separator 6 installed at the top of the reactor. At this time, the carrier is separated from the discharged water in the carrier blocking tube (7) made of a hole hole smaller than the carrier, and gas is also introduced into the treated water outlet (11) by the gas blocking plate (4) located below the carrier blocking tube. It is blocked and discharged out of the reaction tank through the upper gas outlet 10. Solids accumulated in the carrier layer over time are periodically removed by backwashing the carrier layer using only air. Such backwashing is simple and easy by fluidizing the carrier by operating the air blower 18, typically 1-6 times a day, 3-5 minutes per time. The volume control of the sludge layer 9 accumulated under the carrier layer can be easily solved by adjusting the carrier filling amount and the height of the gas acid pipe 5 and controlling the number and duration of backwashing, but if the amount of sludge is excessively large, In this case, if it is impossible to control only by the above method, a sludge drain facility in the form of a conventional sludge settling tank may be further included at the bottom of the reactor.

In the present invention, in addition to the operation method as an auxiliary operation method for maximizing the reaction efficiency of the anaerobic tank, the amount of BOD concentration is lower than the anaerobic effluent, and the final effluent water in the front end of the anaerobic tank (excess of wastewater inflow) 2 times or more), it is proposed to further increase the removal efficiency. In other words, if the final effluent is mixed with the raw water, the load of BOD flowing into the reactor is not increased but the concentration of toxic components in the reactor is further lowered due to the dilution effect of the influent to increase the inactivation of microorganisms. This leads to an increase in reactor removal efficiency. In addition, as the flow rate increases, the HRT in the reactor decreases, which increases the specific activity by lowering the age of the biofilm attached to the carrier, which leads to an increase in the visible removal efficiency.

If the concentration of the wastewater is extremely high or the highly toxic wastewater is contained and the problem of the death of microorganisms in the reactor when operating in the form of a fixed bed tubular reactor is a fluidized mixed reactor is advantageous. In this case, the reaction tank may be stirred using a mechanical stirrer. More preferably, the anaerobic tank exhaust gas may be continuously recycled to the reactor for 24 hours to stir the carrier to operate the fluidized bed. For this fluidized bed operation it is advantageous to lower the position of the gas diffuser 5 in FIG. 1 to be located at the bottom of the reactor (7-15% point) and to use a larger amount of carrier.

Such a method of operating the fluidized bed anaerobic reactor of the present invention will be described in more detail.

In order to fluidize the carrier layer existing as the fixed bed, anaerobic gas discharged to the upper part of the reactor is injected into the reactor by using the valve 19 and the blower 18. The injected gas flows upward through the gas acid pipe 5 located at the bottom of the reaction tank to stir and fluidize the carrier. The wastewater introduced through the liquid distribution pipe 4 under the reactor is removed by the fluidized carrier and sludge, and the treated wastewater passes through the GLM separator 6 and is separated from the gas and the carrier in turn, and then treated water. It is discharged to the outlet 11. The anaerobic gas is separated from the treated water by the gas barrier plate 8 and discharged to the upper gas outlet 14 of the reactor, and part is recycled into the reactor by the blower 18, and the excess anaerobic gas 14 is discharged out of the reactor. do.

In the fluidized bed anaerobic reaction tank of the present invention, when the specific gravity of the carrier is adjusted closer to water, complete fluidization occurs even when the carrier is filled near 90% by volume, and the reaction efficiency is excellent. There is no need to artificially upload. However, if you want to reduce the amount of carrier and increase the amount of sludge instead, if you adjust the carrier density to more than 0.99, even if a very small amount of gas is injected, the carrier is fluidized, but the sludge is heavier than water, so that the sedimentation occurs relatively. Concentration is possible. In addition, as in the fixed bed reactor, when the final discharged water at the end of the treatment facility is recycled to the front of the anaerobic reactor, the excess of the influent (more than twice the amount of raw water) is recycled. Malignant wastewater can also be treated biologically if it was not possible.

Hereinafter, the present invention will be described in more detail with reference to specific examples according to the type of wastewater. However, since these examples are only for illustrating the present invention in more detail, it is obvious to those skilled in the art that the scope of the present invention is not limited by these examples. It will be one day.

<Example 1> be a high-concentration waste water treatment contains an acidic nitrogen

A cylindrical reactor (working diameter 300 mm, height 1,800 mm, water surface height 1,400 mm) designed as shown in FIG. 1 was used to treat wastewater with 7,800 ppm BOD and 2,400 ppm nitrate from the caprolactam manufacturing process. A carrier (7 mm in diameter, 10 mm in length, 800 m ² / m ^{3 in} diameter) of a hollow tube chip type adjusted to specific gravity 0.985 by mixing PE and an inorganic material was introduced into the reactor by 50% by volume. Air was used for backwashing, and air diffusers were installed below the carrier layer 100 mm. The flow rate was set to 1.0 days of HRT for the effective volume of the reactor and denitrification was carried out in a fixed bed reactor. After 2 months of operation, the TN removal rate reached 95% at steady state.

Example 2 Treatment of High Concentration Organic Nitrogen-Containing Wastewater

Concentrated amine and aniline wastewater (CODcr = 8,500 ppm, BOD5 = 3,200 ppm, NH4 + = 40 ppm, organic nitrogen = 1,000 ppm) discharged from the chemical plant was added to the reaction tank used in Example 1 The fixed bed tubular reactor was operated, and backwashing of the carrier layer was performed by switching to a fluidized bed by injecting air for 4 minutes once a day for 5 minutes. For the removal of BOD and nitrification of ammonia, 60 vol% of the same carrier was injected into the reactor 1.5 times as large as the reactor in the back of the anaerobic tank, followed by continuous infusion of air for 24 hours to connect the aerobic tank in series. And operated together. The aerobic tank discharge was carried back to the front of the anaerobic tank with the HRT set to anaerobic tank 2 days and the aerobic tank 3 days. At this time, the treatment result according to the ratio of the return flow rate to the flow rate of the raw water is shown in Figs.

As shown in Figure 3, the COD removal rate of the anaerobic tank increases as the return cost increases, and when the return cost is 6, more than 95% of the anaerobic tank can be removed. Figure 4 shows the effect of ammonification conversion, denitrification and nitrification of organic nitrogen to NH ₄ ⁺ in the aniline and amine structures, when there is no return, only ammonificatin occurs in the anaerobic tank and only nitrification occurs in the aerobic tank. However, it can be seen that the denitrification reaction proceeds simultaneously in addition to the anaerobic digestion and ammonification reaction in the anaerobic tank when the return cost of the back-end aerobic tank treated water is 2 or more. This suggests that if only the return is sufficient, a breakthrough operation capable of simultaneously performing anaerobic, ammonification and denitrification with only one anaerobic tank of the present invention is possible.

<Example 3> second process of the high concentration of chemicals, waste water

Novolac and formaldehyde containing high concentration wastewater (CODMn = 125,000 ppm, BOD 115,000 ppm) from the chemical industry were treated in an anaerobic-aerobic system including the anaerobic tank of the present invention. Anaerobic tank is 70% by volume of the carrier in the anaerobic tank (300 mm in diameter, 1,800 mm in height, working volume = 100 L) shown in Figure 1 and the back of the anaerobic gas released after anaerobic injection into the reaction tank for 24 hours continuously The injection was operated in a fluidized bed mixed reactor, or in a fixed bed tubular reactor without gas injection, but a timer was installed in a gas blower for backwashing, and the gas was injected 6 times a day for 5 minutes. An aerobic tank, in which air was continuously injected for 24 hours instead of anaerobic gas, was installed in series at the rear end of the anaerobic tank in the same reactor as the anaerobic tank. The results of the treatment of the wastewater according to the ratio of the return of the aerobic tank discharge water to the anaerobic tank front as compared to the inflow wastewater after operating the HRT of each reactor for 8 days are shown in Table 1 below. Compared to the fluidized bed mixed reactor, the fixed bed reactor had a lower removal rate, which ultimately caused a problem of microbial death and the reaction efficiency was not stabilized, but the removal rate was maintained high when the carrier ratio increased to 6 or more. The fluidized bed reactor was able to operate stably even with a low return ratio.

<Table 1> Removal rate (%) in anaerobic tank according to return cost

Anaerobic Reactor Operation Type Return fee 0 2 4 6 8 Fixed Bed Tubular Unsafe Instability 60 95 98 Fluid Bed Mixed Type 70 80 90 95 98

As can be seen from the above, the present invention can be converted into a fixed bed tubular reactor or a fluidized bed mixed reactor if necessary, and even when used as a fixed bed reactor, the backwashing of the carrier layer is made of only a short time supply of air, and sludge from the outside. There is no need for re-conveying, and it is easy to operate, so it can easily treat high concentration and high toxicity wastewater with high efficiency.

In addition, when the fluidized bed is operated, the carrier amount can be increased without conveying or accumulating the sludge, and when the specific gravity of the carrier is adjusted to 0.99 or more, the carrier can be fluidized while the sludge has accumulated.

In addition, the anaerobic reaction tank according to the present invention can increase the treatment efficiency by adjusting the conveyed amount of the after-treatment water, and further denitrification is possible when the conveyed amount is increased more than two times.

Claims (39)

A carrier layer made of a floating floating carrier is formed on the surface of the reactor, and the carrier layer is selectively fluidized. The reactor is a biological reactor, characterized in that a separator for separating the gas and the carrier from the discharged treated water. The biological reactor according to claim 1, wherein the carrier has a specific gravity of 0.95 or more and less than 1.0, thereby allowing submerged floating under water. The biological reactor according to claim 1, wherein the carrier is filled with a predetermined thickness on the surface of the reactor to form a fixed carrier layer. 4. The biological reactor according to claim 3, wherein the carrier layer is filled with 2-90% by volume of the reactor. The biological reactor according to any one of claims 1 to 3, wherein the carrier layer is fluidized by an acidic device. The biological reactor according to claim 5, wherein the acid diffuser is formed between the fixed carrier layer and the sludge layer. The biological reactor of claim 1, wherein the carrier layer is intermittently fluidized upon backwashing of the carrier layer. The biological reactor of Claim 1, wherein the carrier bed is continuously fluidized to operate as a fluidized bed. delete The biological reactor of Claim 1, wherein the separator is installed to be submerged under the water surface layer. Reactor; A stationary bed carrier layer consisting of a submerged floating carrier is formed on the surface of the reactor, and the carrier layer can be selectively fluidized; Diffuser device; A liquid distribution tube for introducing and discharging wastewater into the reactor tank; And In the biological anaerobic tank comprising a treated water separator for separating and discharging the gas and the carrier from the treated water passed through the carrier layer, The biological anaerobic tank is operated in a fluidized bed or a fixed bed in accordance with the operation of the acidic device. The method of claim 11, The treatment water separator is installed to be submerged under the surface layer of the water surface, and a tubular carrier blocking tube having a plurality of holes smaller than the carrier size is formed integrally with the carrier blocking tube, and has a '∧' shape. Biological anaerobic reactor comprising a blocking plate, each separating the carrier and gas from the treated water to discharge only the treated water into the carrier blocking tube. The method of claim 11, The acidic device is installed under the carrier layer is a biological anaerobic reactor, characterized in that installed to fluidize the carrier during gas injection. The method of claim 11, The carrier is a biological anaerobic reactor characterized in that the specific gravity is adjusted to more than 0.95 and less than 1.0, the length of the cross-section is 2-50mm. The method of claim 11, The carrier layer is a biological anaerobic reactor, characterized in that to form a 2-90% by volume in the tank tank. The method of claim 11, The liquid distribution pipe is installed in the lower portion of the reaction tank tank biological anaerobic reactor, characterized in that the reaction by flowing the influent wastewater upstream. The method of claim 11, A biological anaerobic gas is formed in the upper part of the reactor tank for discharging the anaerobic gas, and a blower for recycling some of the anaerobic gas discharged through the outlet into the reactor tank is installed in communication with the diffuser device. Reactor. 18. The biological anaerobic reactor according to claim 17, wherein water having a lower BOD concentration than wastewater treated with the reactor tank is introduced at the front of the sedimentation tank. delete 19. The biological anaerobic reactor according to claim 18, wherein the water having a low BOD concentration is introduced in an excess amount of two times or more than waste water. delete delete delete delete delete delete Reactor; A carrier layer having a specific gravity of 0.95 or more and 1.0 or less composed of a floating floating carrier on the surface of the reactor; An acidic device for selectively fluidizing the carrier layer; A liquid distribution tube for introducing and discharging wastewater into the reactor tank; And a biological anaerobic tank comprising a treated water separator for separating and discharging the gas and the carrier from the treated water passing through the carrier layer, wherein the wastewater is selectively treated as a fixed bed or a fluidized bed. 28. The method of claim 27, wherein the treated water separator is submerged under the surface layer of the water, the tubular carrier blocking tube formed with a plurality of holes smaller than the carrier size, and integrally formed under the carrier blocking tube ' Biological wastewater treatment method comprising a gas barrier plate having a '' shape, respectively separating the carrier and gas from the treated water to discharge only the treated water into the carrier blocking tube. 29. The method of claim 27, wherein the acidic device is formed under the carrier layer. 28. The method of claim 27, wherein the biological anaerobic tank causes a reaction by flowing the influent wastewater in an upflow when operating in a fixed bed, and periodically passes gas through an air diffuser located below the carrier layer with the carrier layer contaminated with solids as the reaction time elapses. Injecting the waste water treatment method characterized in that the backing by fluidizing the carrier layer. The wastewater treatment method according to claim 27, wherein the biological anaerobic tank is operated by continuously operating an acidic device to fluidize the carrier layer and sludge. 28. The method of claim 27, wherein the wastewater is operated in a fluidized bed when the concentration of the wastewater is high or highly toxic. The wastewater treatment method according to claim 27, wherein the downstream treatment water having a lower BOD concentration than the wastewater treated by the reactor tank is introduced and treated together. delete  34. The wastewater treatment method of claim 33, wherein the aftertreatment water is introduced in an excess of twice as much as the wastewater. 36. The wastewater treatment method according to claim 35, wherein the aftertreatment water is introduced in an excess of two or more than the wastewater to cause a denitrification reaction. 32. The wastewater treatment method according to claim 31, wherein the carrier is charged in an amount of 70 to 90% by volume to operate without sludge conveying. 32. The wastewater treatment method according to claim 31, wherein the specific gravity of the carrier is adjusted to 0.99 or more so that the sludge is filled at the bottom of the reactor while the carrier is flowed by an acid group. It is installed to be submerged under the surface layer of the water surface, and consists of a tubular carrier blocking tube having a plurality of holes smaller than the carrier size, and a gas barrier plate integrally formed at the lower part of the carrier blocking tube and having a ',' shape. And a carrier and a gas, respectively, from the treated water to discharge only the treated water into the carrier barrier tube.

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