WO2016182351A1 - Diffuser for sewage/waste water treatment apparatus, and method for manufacturing same - Google Patents

Abstract

The present invention relates to a sewage/waste water treatment apparatus, and more specifically, a diffuser for a sewage/waste water treatment apparatus for purifying sewage or waste water using bubbles in the sewage or waste water, and a method for manufacturing same. Disclosed is a diffuser for a sewage/waste water treatment apparatus which increases dissolved oxygen in sewage and waste water using aeration bubbles, performs sedimentation, and then floats particles in the sewage or waste water using microbubbles, wherein the diffuser, as a diffuser forming 90% or more of aeration bubbles having a diameter of 0.5 mm to 5 mm, is manufactured by mixing water and a mixture comprising SiO2, Al2O3, starch, and inevitable impurities as a remainder, kneading the resulting mixture, then molding and firing.

Description

Diffusion engine of sewage water treatment system and its manufacturing method

The present invention relates to a wastewater treatment apparatus, and more particularly, to an diffuser and a manufacturing method of a wastewater treatment apparatus for purifying sewage or wastewater using air bubbles in sewage or wastewater.

In biological sewage treatment processes to remove organic matter, nitrogen and phosphorus in sewage, a collection of microorganisms called activated sludge is a biological solid that plays a key role.

The operating efficiency of the sewage treatment process (activated sludge process) using activated sludge depends on the concentration load and flow load of pollutants including organic matter of the influent sewage, the activated sludge concentration and state of the reactor, the hydraulic residence time and the solid residence time. It is greatly affected.

In particular, the concentration of activated sludge has been recognized as a very important driving factor not only in typical activated sludge processes but also in advanced sewage treatment processes including nitrogen and phosphorus removal.

However, gravity sedimentation, which is most commonly used among the existing solid-liquid separation methods, cannot properly adjust or maintain the activated sludge concentration in the reactor.

In particular, sludge swelling caused by intermittent sludge bulking or sedimentation during sludge, sludge re-injury caused by nitrogen gas deterioration, consequent deterioration of solid-liquid separation efficiency and excessive loss of activated sludge are best addressed in gravity settling. It is pointed out as a difficult problem.

The methods developed for the operation of a high concentration activated sludge process include an activated sludge process (Membrane Bioreactor, MBR) using an immersion membrane, a pure oxygen aeration process, and a biofilter method using a carrier which is a typical deposition growth method.

When microorganisms are maintained at high concentration in activated sludge process, the organic matter load per unit volume can be increased by increasing the organic matter treatment capacity in the aeration tank, which can reduce the reaction tank volume by 50 ~ 75%, and thus the required site area. Also greatly reduced.

In addition, the nitrification rate is expected to be sharply improved according to the increase in the nitric oxide microbial concentration, it is possible to maximize the removal efficiency of ammonia nitrogen.

In addition, due to the low F / M ratio (food-to-microorganism ratio), the self-oxidation of sludge is actively progressed and the amount of excess sludge is expected to decrease.

However, in the case of the MBR process or the biofilter method, the initial cost according to the purchase of the membrane or the carrier is very large, and the blockage by activated sludge or sludge secretion occurs during a long period of operation, thereby increasing the pressure loss.

Therefore, there is a disadvantage in that periodic cleaning or backwashing must be accompanied.

In the case of aeration using pure oxygen, stable sedimentation of the sludge must be ensured at all times in order to maintain activated sludge at a high concentration. Known.

In addition, there is a disadvantage in that additional costs are required to supply oxygen.

In addition to these methods, a continuous batch process in which a unit process of fill, reaction, settling, draw and idle of sewage and the like in a single reactor is continuously performed according to a predetermined time sequence. A sequencing batch reactor (SBR) process has been developed and applied to wastewater treatment.

This method is not only unnecessary secondary sedimentation basin because each unit process is performed in a single reactor, it is easy to control filamentous bacteria and easy construction, which is very advantageous in terms of stable management of sewage.

However, this typical or modified form of SBR process is not only able to keep the mixed liquor suspended solids (MLSS) concentrations as high as desired, but also requires a long time for the precipitation reaction, which is almost essential to complete the entire process. The disadvantage is that the cycle time is increased.

In addition, the existing SBR process has a disadvantage that the sludge particles are included in the effluent when the water flow characteristics in the reaction vessel is changed in the process of flowing out the treated water.

In addition, since blowers are used in most existing aeration processes, the use of a large amount of power has caused a problem due to an increase in the cost of maintenance of the process.

Meanwhile, in order to shorten the time required for securing the microbial concentration and the precipitation reaction of the reactor, a flotation method may be used, and among these, dissolved air flotation (DAF) is widely used as a prior art.

However, the dissolved air flotation method requires a high pressure of 4-5 atm to supply dissolved air and a large-capacity compression device to secure the air volume. There are disadvantages.

In order to overcome this drawback, air flotation (AF), which is recently used, generates bubbles by using ceramic membrane diffusers instead of generating bubbles by using dissolved dissolved air. The solid-liquid flotation is separated, and the high-liquid sludge separated from the solid-liquid is transported and removed by a skimmer.

On the other hand, the sewage treatment apparatus by air flotation method, as shown in Figure 1, performs the precipitation process, and after performing the aeration process one or more times to increase the amount of dissolved oxygen by using the air bubbles again after performing the precipitation process fine bubbles Injury process to injure the sludge and remove it can be performed sequentially.

Here, the aeration process and the flotation process are performed through the diffuser formed pores.

However, the conventional wastewater treatment apparatus using the air flotation method has a problem in that it is difficult to manufacture a diffuser suitable for performing the aeration process and the flotation process, so that the wastewater treatment method using the air flotation method is commercialized.

SUMMARY OF THE INVENTION An object of the present invention is to provide a diffuser and a manufacturing method of a wastewater treatment apparatus capable of forming bubbles capable of providing an optimal aeration effect in order to solve the above problems.

The present invention was created in order to achieve the object of the present invention as described above, the present invention, sewage or waste water to increase the amount of dissolved oxygen using aeration bubble, and after the precipitation process using sewage or fine bubbles A wastewater treatment apparatus that floats particles in wastewater, the diffuser forming an aeration bubble having a diameter distribution of 0.5 mm to 5 mm or more and 90% or more, comprising SiO ₂ , Al ₂ O ₃ , starch, and remainder as inevitable impurities. Disclosed is a diffuser of a wastewater treatment apparatus manufactured by mixing and kneading a mixture with water and then molding and baking.

The mixture may include one or more of Fe ₂ O ₃ , CaO, MgO, Actigel, micelles, and PEO.

The mixture is 49wt% to 60wt% SiO ₂ , 28wt% to 41wt% Al ₂ O ₃ , 0.5wt% to 1.5wt% Fe ₂ O ₃ , 0.1wt% to 0.6wt% CaO, 0.05wt% As 0.3 wt% MgO, 0.1 wt% to 0.4 wt% etigel, 0.1 wt% to 0.4 wt% micelles, and 0.1 wt% to 0.4 wt% PEO, 3 wt% to 13 wt% starch, and the balance May contain unavoidable impurities.

Actigel is a product of Active Minerals (http://activeminerals.com/) and is defined as hydrous magnesium aluminum-silicate.

Micelles, also referred to as micelles, refer to aggregates in which surfactants are aggregated above a certain concentration.

After kneading the mixture, it may be formed as a molded body by extrusion molding and then formed by drying and firing.

Firing of the molded body may be performed under a temperature of 900 ℃ ~ 1,400 ℃.

The diffuser has a length between 20 cm and 200 cm, and air may be injected at an air pressure between 0.09 MPa and 0.2 MPa.

The present invention also increases the amount of dissolved oxygen in the sewage or waste water by using aeration bubbles, and in the sewage treatment apparatus for floating particles in sewage or waste water using fine bubbles after the precipitation process, the diameter distribution is 0.5mm ~ A method for producing an diffuser that forms an aeration bubble of 5% or more at 5 mm, wherein a mixture containing SiO ₂ , Al ₂ O ₃ , starch, and unavoidable impurities as remainder is mixed with water and kneaded, followed by molding and firing Disclosed is a method of manufacturing an diffuser of a manufactured sewage water treatment apparatus.

The diffuser and the method of manufacturing the wastewater treatment apparatus according to the present invention, by providing a composition of the mixture for the formation of the diffuser forming the aeration bubbles, it is possible to form aeration bubbles that can give an optimum aeration effect There is an advantage to that.

1 is a block diagram showing an example of a treatment process of a wastewater treatment apparatus using an air flotation method.

2 is a conceptual diagram showing a part of a wastewater treatment apparatus according to the present invention.

3 is a perspective view showing one embodiment of the diffuser in FIG.

Figure 4 is a graph showing the distribution of the diameter of the bubble for aeration formed by the diffuser formed by the composition of the conditions according to the present invention as the diffuser of FIG.

5 is a graph showing the amount of air discharged by injection pressure (MPa).

Hereinafter, the diffuser and the manufacturing method of the wastewater treatment apparatus according to the present invention will be described with reference to the accompanying drawings.

The diffuser 2 of the wastewater treatment apparatus according to the present invention, as shown in Figures 2 and 3, is installed in the bottom portion of the septic tank 1 containing the sewage or wastewater to form bubbles in the sewage or wastewater to sewage Or to increase the amount of dissolved oxygen in the wastewater.

Here, the wastewater treatment apparatus forms aeration bubbles at the bottom of the septic tank 1 containing the sewage or wastewater, that is, increases the amount of dissolved oxygen in the sewage or wastewater by using the bubbles to secure microbial concentration and settling reactions. It is a device for shortening the time and purifying sewage or wastewater by removing particles, etc. deposited after the aeration process using fine bubbles.

And the diffuser (2) has a certain length so as to form a bubble for aeration in the bottom portion of the septic tank (1) containing the sewage or waste water is connected to the main pipe (3) connected to the air supply device, such as an air pump It may have a pipe shape.

In detail, the diffuser 2 has a length between 20 cm and 200 cm, and air may be injected at an air pressure between 0.09 MPa and 0.2 MPa.

Here, the diffuser 2 may be configured as a hollow cylinder having one end connected to the main pipe 3 described above and the other end blocked.

In addition, the diffuser (2) may be arranged parallel to each other on both sides with respect to the main pipe (3).

On the other hand, the diffuser (2), according to the experiment, confirms the best effect of increasing the amount of dissolved oxygen when forming an aeration bubble having a diameter distribution of more than 90% at 0.5mm ~ 5mm under the conditions of air pressure between 0.09MPa ~ 0.2MPa It was.

In particular, it is preferable that the said bubble for aeration is 2 mm in average diameter.

Thus, the diffuser 2 is preferably manufactured to form an aeration bubble having a diameter distribution of 90% or more at 0.5mm to 5mm under conditions of air pressure between 0.09MPa and 0.2MPa.

The present inventors present the composition and firing conditions of the mixture for forming the diffuser 2, the diffuser 2, forming a bubble for aeration having a diameter distribution of more than 90% at 0.5mm ~ 5mm. As the diffuser, it is preferable that the mixture containing SiO ₂ , Al ₂ O ₃ , starch, and the remainder as an unavoidable impurity is mixed with water and kneaded, followed by molding and firing.

As a specific manufacturing process, the acid pipe (2) is a mixture of SiO ₂ , Al ₂ O ₃ , starch, unavoidable impurities as a balance to form a mixture, adding water to the mixed mixture through the mixing process Kneading process by kneading, molding process of forming the diffuser 2 to a diameter and length predesigned after the kneading process, drying process of drying the molded body through the molding process, and heating the molded body after the drying process to a predetermined temperature By firing can be prepared through a firing process.

The mixing process and the kneading process may be merged with each other depending on the time of the water input, the amount of water to be added may be selected in an appropriate amount in consideration of the molding conditions.

The molding process is a process of molding the diffuser 2 to a diameter and length previously designed after kneading, and is preferably extruded in consideration of having an empty hollow cylinder structure inside.

The firing process may be performed by various processes as a process of heating and baking a molded product that has undergone a drying process and a drying process at a temperature of 900 ° C to 1,400 ° C.

On the other hand, the diffuser (2), the diameter distribution of the aeration bubbles formed by the adjustment of the mixture is determined, at least one of Fe ₂ O ₃ , CaO, MgO, actigel, micelles, and PEO (polyethylene oxide) It is more preferable to include.

In particular, if the composition in the actigel <0.1wt% or PEO <0.1wt%, the pressure of the extruder is operated at a high load, the wear of the extrusion equipment is severe, there is a problem that the productivity is rapidly reduced (50% or more) due to the extrusion speed decrease.

In addition, if the actigel> 0.4wt% or PEO> 0.4wt%, the formation of the molding is weak, and there is a problem that the warpage of the molding occurs during the drying process.

However, in the case of 0.1wt% ~ 0.4wt% of actigel and 0.1wt% ~ 0.4wt% PEO it was confirmed that the above problems are significantly improved.

In addition, if the micelle <0.1wt%, there is a problem of cracking during firing of the molding, and if the micelle <0.4wt%, the wear of the equipment is severe due to overload of the refining and extrusion systems, and the productivity is rapidly deteriorated. There is this.

However, in the case of micelles of 0.1wt% ~ 0.4wt%, it was confirmed that the above problems are remarkably improved.

In addition, the diffuser 2 needs to be optimized for the composition of the mixture so as to form aeration bubbles having a diameter distribution of 90% or more at 0.5 mm to 5 mm under conditions of air pressure between 0.09 MPa and 0.2 MPa. .

Thus, the mixture is a weight ratio excluding water, 49wt% ~ 60wt% SiO ₂ , 28wt% ~ 41wt% Al ₂ O ₃ , 0.5wt% ~ 1.5wt% Fe ₂ O ₃ , 0.1wt% ~ 0.6 wt% CaO, 0.05wt% ~ 0.3wt% MgO, 0.1wt% ~ 0.4wt% Actigel, 0.1wt% ~ 0.4wt% Micell, and 0.1wt% ~ 0.4wt% PEO, 3wt% ~ It is preferable to contain 13 wt% of starch, and remainder as unavoidable impurities.

For reference, according to the experiment, when the diameter distribution of the aeration bubble is more than 90% at 0.5mm ~ 5mm, it is possible to optimize the effect of increasing the amount of dissolved oxygen.

It is preferable that especially the diameter of the bubble for aeration is 1.0 mm-3.0 mm. If the diameter of the bubble for aeration is smaller than 1.0mm, there is a problem that the slurry containing the organic material including nitric acid, phosphorus, etc. is floated to the surface layer, if larger than 3.0mm there is a problem that rises immediately to the dissolved oxygen increase effect is reduced. .

Example

The composition of the mixture was 55 wt% SiO ₂ , 35 wt% Al ₂ O ₃ , 1.5 wt% Fe ₂ O ₃ , 0.6 wt% CaO, 0.3 wt% MgO, 0.35 wt% Actigel, 0.35 wt% Micelles, 0.35 wt% PEO, 6 wt% starch, and the balance were unavoidable impurities.

Then, water was added to the mixture to knead, extruded, and formed by drying and baking.

After firing, the diffuser 2 was formed with a hollow inner diameter D ₂ of 2.6 cm, an outer diameter D ₁ of 4 cm, and a length of 120 cm.

Injecting air to the diffuser 2 at a pressure of 0.12 MPa and measuring the aeration bubbles formed in the septic tank, aeration bubbles are formed under the conditions of the graph as shown in FIG. (MPa) The amount of air released was confirmed.

4, it can be seen that the aeration bubbles formed by the diffuser 2 have a diameter distribution of more than 90% at a diameter of 0.5 mm to 5 mm.

Therefore, under the conditions of the mixture as described above, when forming the diffuser (2), the aeration bubbles are 90% or more in diameter distribution of 0.5mm ~ 5mm, aeration bubbles that can give the optimum dissolved oxygen increase effect It can be seen that they can form.

That is, according to the experiment of the present invention, the aeration bubbles are more than 90% at a diameter distribution of 0.5mm ~ 5mm, according to the composition conditions described above in forming aeration bubbles that can give an optimum dissolved oxygen increase effect It can be seen that it is implemented.

Since the above has been described only with respect to some of the preferred embodiments that can be implemented by the present invention, the scope of the present invention, as is well known, should not be construed as limited to the above embodiments, the present invention described above It will be said that both the technical idea and the technical idea which together with the base are included in the scope of the present invention.

Claims (12)

1. In the sewage treatment apparatus for increasing the dissolved oxygen amount of the sewage or waste water by using the aeration bubble, and after the sedimentation process to float the particles in the sewage or waste water by using fine bubbles,

   An diffuser that forms aeration bubbles with a diameter distribution of 0.5mm to 5mm or more and 90% or more.

   A diffuser of a wastewater treatment apparatus manufactured by molding and firing after mixing a mixture containing SiO ₂ , Al ₂ O ₃ , starch, and unavoidable impurities as remainder with water.
2. The method according to claim 1,

   The mixture is Fe ₂ O ₃ , CaO, MgO, Actigel, micelles, and the diffuser of the sewage treatment apparatus, characterized in that it comprises at least one of PEO.
3. The method according to claim 1,

   The mixture is 49wt% to 60wt% SiO ₂ , 28wt% to 41wt% Al ₂ O ₃ , 0.5wt% to 1.5wt% Fe ₂ O ₃ , 0.1wt% to 0.6wt% CaO, 0.05wt% As 0.3 wt% MgO, 0.1 wt% to 0.4 wt% etigel, 0.1 wt% to 0.4 wt% micelles, and 0.1 wt% to 0.4 wt% PEO, 3 wt% to 13 wt% starch, and the balance The diffuser of the sewage treatment apparatus, comprising inevitable impurities.
4. The method according to any one of claims 1 to 3,

   A diffuser of the wastewater treatment apparatus, characterized in that the mixture is formed as a molded body by extrusion molding and then dried and baked.
5. The method according to any one of claims 1 to 3,

   Firing of the compact, the diffuser of the wastewater treatment apparatus, characterized in that carried out at a temperature of 900 ℃ ~ 1,400 ℃.
6. The method according to claim 5,

   The diffuser has a length between 20 cm and 200 cm and air is injected into the air pressure between 0.09 MPa and 0.2 MPa.
7. In the sewage treatment apparatus for increasing the dissolved oxygen amount of the sewage or waste water by using the aeration bubble, and after the sedimentation process to float the particles in the sewage or waste water by using fine bubbles,

   As the manufacturing method of the diffuser which forms the bubble for aeration whose diameter distribution is 90% or more in 0.5mm-5mm,

   A method for producing an acid pipe of a sewage treatment apparatus manufactured by molding and baking after mixing a mixture containing SiO ₂ , Al ₂ O ₃ , starch, and unavoidable impurities as remainder with water.
8. The method according to claim 7,

   The mixture is Fe ₂ O ₃ , CaO, MgO, Actigel, micelles, PEO manufacturing method of the diffuser of the wastewater treatment apparatus, characterized in that it comprises a PEO.
9. The method according to claim 7,

   The mixture is 49wt% to 60wt% SiO ₂ , 28wt% to 41wt% Al ₂ O ₃ , 0.5wt% to 1.5wt% Fe ₂ O ₃ , 0.1wt% to 0.6wt% CaO, 0.05wt% As 0.3 wt% MgO, 0.1 wt% to 0.4 wt% etigel, 0.1 wt% to 0.4 wt% micelles, and 0.1 wt% to 0.4 wt% PEO, 3 wt% to 13 wt% starch, and the balance A method for producing an diffuser of a sewage treatment apparatus, comprising inevitable impurities.
10. The method according to any one of claims 7 to 9,

    And forming a molded body by extrusion molding after kneading the mixture, followed by drying and firing.
11. The method according to any one of claims 7 to 9,

    Firing of the molded body, the manufacturing method of the diffuser of the sewage treatment apparatus, characterized in that carried out at a temperature of 900 ℃ ~ 1,400 ℃.
12. The method according to claim 11,

    The diffuser has a length between 20 cm and 200 cm, and air is injected at an air pressure between 0.09 MPa and 0.2 MPa.

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