阅读说明：本技术 好氧生物处理装置及其运转方法 (Aerobic biological treatment apparatus and method for operating the same ) 是由 深濑哲朗 小林秀树 于 2019-01-28 设计创作，主要内容包括：本发明的好氧生物处理装置(1)包括：反应槽(槽体)(2)；透水板(3),水平设置于该反应槽(2)的下部；大径粒子层(4),形成于该透水板(3)的上侧；小径粒子层(5),形成于该大径粒子层(4)的上侧；氧溶解膜组件(6),配置于该小径粒子层(5)的上侧；接收室(7),形成于该透水板(3)的下侧；原水散布管(8),向该接收室(7)内供给原水；以及在接收室(7)内用于进行散气而设置的散气管(9)等。将流化床(F)的活性碳的平均粒径设为0.2～1.2mm,将LV设为30m/hr以下。(The aerobic biological treatment device (1) of the present invention comprises: a reaction tank (tank body) (2); a water permeable plate (3) horizontally arranged at the lower part of the reaction tank (2); a large-diameter particle layer (4) formed on the upper side of the water permeable plate (3); a small-diameter particle layer (5) formed on the upper side of the large-diameter particle layer (4); an oxygen-dissolving membrane module (6) disposed above the small-diameter particle layer (5); a receiving chamber (7) formed below the water permeable plate (3); a raw water dispersion pipe (8) for supplying raw water into the receiving chamber (7); and a gas diffusion pipe (9) provided in the receiving chamber (7) for diffusing gas. The average particle diameter of the activated carbon in the fluidized bed (F) is set to 0.2 to 1.2mm, and LV is set to 30m/hr or less.)

1. An aerobic biological treatment device comprising:

a reaction tank;

a fluidized bed carrier which is filled in the reaction tank and has an average particle size of 0.2-0.6 mm;

an oxygen dissolving membrane module disposed in the reaction tank with the aeration direction being the vertical direction;

an oxygen-containing gas supply system for supplying an oxygen-containing gas to the oxygen dissolving membrane module; and

and a water system for introducing raw water into the reaction tank in an upward flow mode.

2. The aerobic biological treatment device according to claim 1, wherein the fluidized bed carrier is activated carbon.

3. The aerobic biological treatment device according to claim 1 or 2, wherein the oxygen dissolving membrane is a hollow fiber membrane.

4. A method of operating an aerobic biological treatment apparatus according to any one of claims 1 to 3, wherein raw water is introduced in an upward flow manner at a linear velocity of 7 to 30 m/hr.

Technical Field

The invention relates to an aerobic biological treatment device for organic drainage and an operation method thereof.

Background

Since the aerobic biological treatment method is inexpensive, it is often used as a treatment method for organic wastewater. In this method, oxygen needs to be dissolved in the water to be treated, and aeration is usually performed by using a diffuser pipe.

The dissolution efficiency is low when aeration is carried out by using the air diffusing pipe, and is about 5-20%. Further, it is necessary to perform aeration at a pressure higher than the water pressure received in the deep water space where the air diffuser is installed, and a large amount of air is blown by high-pressure blowing, which results in a high cost of electric power for the blower. Generally, two thirds or more of the electricity cost in aerobic biological treatment is used for oxygen dissolution.

A membrane-aerated biofilm reactor (MABR) using a hollow fiber membrane enables oxygen dissolution without generating bubbles. In the MABR, since air having a pressure lower than the water pressure applied to the water depth is introduced, the blower has a low pressure required and the oxygen dissolving efficiency is high.

Patent document 1: japanese patent laid-open No. 2006-87310.

Disclosure of Invention

The invention aims to provide an aerobic biological treatment device and an operation method thereof, wherein the amount of biological adhesion on a fluidized bed carrier is large, and high biological treatment efficiency can be maintained for a long time.

The aerobic biological treatment apparatus of the present invention comprises: a reaction tank; a fluidized bed carrier which is filled in the reaction tank and has an average particle size of 0.2-1.2 mm; an oxygen dissolving membrane module disposed in the reaction tank with the aeration direction being the vertical direction; an oxygen-containing gas supply system for supplying an oxygen-containing gas to the oxygen dissolving membrane module; and a water system for introducing raw water into the reaction tank in an upward flow manner.

In one embodiment of the present invention, the fluidized bed carrier is activated carbon.

In one embodiment of the present invention, the dissolution membrane is a non-porous hollow fiber membrane.

In the operation method of the aerobic biological treatment device, raw water is introduced in an upward flow manner at a Linear Velocity (LV) of 7-30 m/hr.

[ Effect of the invention ]

In the present invention, since the average particle diameter of the fluidized bed carrier is reduced to 1.2mm or less, the specific surface area of the fluidized bed carrier is large. Therefore, the biofilm area is large, and the load and energy of the treatment can be increased. Further, since the average particle diameter of the fluidized bed carrier is set to 0.2mm or more, the fluidized bed carrier has a high cleaning effect on the oxygen dissolving membrane, and can prevent the adhesion and propagation of organisms on the surface of the oxygen dissolving membrane.

Drawings

FIG. 1 is a longitudinal sectional view of a biological treatment apparatus according to an embodiment.

Fig. 2(a) is a side view of the oxygen dissolving membrane unit, and fig. 2(b) is a perspective view of the oxygen dissolving membrane unit.

Detailed Description

The present invention will be described in more detail below with reference to the accompanying drawings.

FIG. 1 is a longitudinal sectional view of an aerobic biological treatment apparatus 1 according to an embodiment. The aerobic biological treatment apparatus 1 comprises: a reaction tank (tank body) 2; a water permeable plate 3 such as a perforated plate such as a perforated sheet horizontally disposed at the lower part of the reaction tank 2 or a flat plate having a plurality of dispersing nozzles uniformly disposed thereon; a large-diameter particle layer 4 formed on the upper side of the water permeable plate 3; a small-diameter particle layer 5 formed on the upper side of the large-diameter particle layer 4; a fluidized bed F formed by attaching a fluidized bed carrier to the upper side of the small-diameter particle layer 5 via living organisms such as granular activated carbon; an oxygen dissolution membrane module 6, at least a part of which is disposed in the fluidized bed F; a receiving chamber 7 formed below the permeable plate 3; a raw water distribution pipe 8 for supplying raw water into the receiving chamber 7; and a gas diffusing pipe 9 for supplying a gas for backwashing or the like when cleaning the packed layer. A groove (trough)10 for discharging the treated water and an outlet 11 are provided in the upper part of the reaction tank 2. The groove 10 forms an annular flow path along the inner wall of the groove. The fluidized bed carrier is preferably activated carbon having an average particle diameter of 0.2 to 1.2mm, particularly 0.3 to 0.6 mm. The particle diameter of the carrier is a value measured using a JIS sieve.

In fig. 1, the fluidized bed carrier is filled in the reaction tank, and the adhesion of the biofilm to the surface of the oxygen dissolving membrane is suppressed by the shear force generated by the carrier flow, so that most of the biofilm adheres to the fluidized bed carrier, and at this time, the oxygen dissolving membrane is used only for the purpose of oxygen supply. Since the average particle diameter of the carrier is 0.2mm or more, the shearing force applied to the surface of the oxygen-dissolved film by the flowing carrier becomes large, and the adhesion and propagation of organisms are prevented. Further, the average particle diameter of the carrier is set to 1.2mm or less, so that the specific surface area of the carrier becomes large, the amount of the biofilm to be attached becomes large, and sufficient biological treatment can be performed.

In the configuration shown in FIG. 1, a non-porous (non-porous) oxygen-dissolved membrane is used as the oxygen-dissolved membrane, and oxygen-containing gas is introduced from the outside of the tank to the primary side of the oxygen-dissolved membrane through a pipe, and exhaust gas is discharged from the tank through the pipe. Therefore, the oxygen-containing gas is introduced into the oxygen-dissolved film at a low pressure, and oxygen passes through between the constituent atoms of the oxygen-dissolved film (dissolved in the film) as oxygen molecules and contacts the water to be treated as oxygen molecules. Since oxygen is directly dissolved in water, bubbles are not generated. The above method uses a mechanism of molecular diffusion by a concentration gradient, and it is not necessary to perform air diffusion by an air diffusion tube or the like as in the conventional method.

Further, it is preferable to use a hydrophobic material as the material of the oxygen-dissolving film because in this case, the film is not easily soaked with water. However, even a hydrophobic film cannot prevent entry of a slight amount of water vapor.

Fig. 2 shows an example of the oxygen dissolving membrane module 6. The oxygen dissolving membrane module 6 uses a non-porous hollow fiber membrane 22 as the oxygen dissolving membrane. In the present embodiment, the hollow fiber membranes 22 are arranged in a vertical row, and the upper end of each hollow fiber membrane 22 is connected to the upper header 20 and the lower end is connected to the lower header 21. The interiors of the hollow fiber membranes 22 communicate with the interior of the upper header 20 and the interior of the lower header 21, respectively. Each of the upper header 20 and the lower header 21 has a hollow tubular shape. In addition, when a flat membrane or a spiral membrane is used, it is preferable that the air flow direction is also arranged in a row in the vertical direction.

As shown in fig. 2(b), a plurality of cells each including a pair of upper headers 20, lower headers 21, and hollow fiber membranes 22 are arranged in parallel and in a row. As shown in fig. 2(a), preferably, the upper portion of each upper header 20 is connected to an upper manifold 23 via a pipe, and the lower portion of each lower header 21 is connected to a lower manifold 24 via a pipe. The oxygen-containing gas is supplied to the upper part of the oxygen-dissolved membrane module 6, and is discharged from the lower part of the oxygen-dissolved membrane module 6. An oxygen-containing gas such as air flows from the upper header 20 to the lower header 21 through the hollow fiber membranes 22, and during this period, oxygen permeates through the hollow fiber membranes 22 and is dissolved in water in the reaction tank 2.

The upper headers 20 and the lower headers 21 and the upper manifolds 23 and the lower manifolds 24 may have a water flow gradient. The oxygen dissolving membrane module 6 may be arranged in a plurality of stages.

An air blower 26 and an air supply pipe 27 for supplying air are provided to supply air to the oxygen dissolving membrane module 6, thereby constituting an oxygen-containing gas supply system. The air supply pipe 27 is connected to the upper manifold 23. A relay pipe 28 for exhaust is connected to the lower manifold 24. A discharge pipe 29 is connected to the relay pipe 28. The discharge pipe 29 is provided to extend to the outside of the reaction tank 2 so as to have an inclined downward direction (including a vertical downward direction). Although the discharge pipe 29 is drawn to the side of the reaction tank 2 in fig. 1, it may be drawn downward from the bottom of the reaction tank 2.

As shown in FIG. 1, the oxygen-containing gas remaining undissolved in the oxygen-dissolved membrane is discharged to the outside of the tank through a discharge pipe 29. The end of the pipe 29 is disposed at a position lower than the lower end of the oxygen-dissolved membrane module 6 (the lowest end of the lower ends of the modules when a plurality of modules 6 are provided). Therefore, when the condensed water is contained in the exhaust gas, the condensed water flows out to the reservoir (tank)32 below the discharge pipe 29. The water in the storage tank 32 may be sent to the reaction tank 2 through a pump 33 and a pipe 34.

In the above configuration, the discharge pipe 29 is configured to discharge the exhaust gas to the outside of the tank and the condensed water to the outside of the tank at the same time, but is not limited thereto. The exhaust pipe 30 for discharging exhaust gas to the outside of the tank may be connected to the exhaust pipe 29 inside or outside the tank. In this case, the condensed water is discharged through the discharge pipe 29. The end of the exhaust pipe 30 may be disposed at a position higher than the lower end of the oxygen dissolving membrane module. In order to prevent the condensed water from being accumulated, the exhaust pipe 30 is preferably configured not to be inclined downward but to be inclined upward or vertically upward. A valve (not shown) may be provided downstream of a branch point of the discharge pipe 29 with respect to the exhaust pipe 30, and the condensed water may be discharged to the sump 32 by opening the valve.

The valve can be an automatic valve or a manual valve. The valve for discharging the condensed water may be opened continuously or intermittently. In the intermittent operation, the valve is opened once every 1 day to 30 days (once every 1 day for several seconds, once every 1 month for several tens of seconds, if any), preferably once every 1 day to 15 days, and the water is discharged.

The filling amount of the fluidized bed carrier is preferably about 30 to 70%, particularly about 40 to 60%, of the volume of the reaction tank. The more the amount of the charged biomass, the more the biomass and the higher the activity, but the more the amount of the charged biomass, the more the carrier may flow out. Therefore, it is preferable to conduct water flow by expanding the fluidized bed to about 20 to 50% LV, for example, about 7 to 30m/hr, particularly about 8 to 15 m/hr. If the deployment rate is less than 20%, clogging and a short path may occur. If the expansion ratio is higher than 50%, the carrier may flow out, and the pump power cost increases.

In general, the spread rate of the fluidized bed of activated carbon is about 10 to 20% for the biological activated carbon, but in this case, the activated carbon flows up, down, left, and right unevenly in the flow state. As a result, the film provided at the same time is rubbed by the activated carbon, and thus is cut and consumed. In order to prevent this, in the present invention, it is necessary to sufficiently flow the fluidized bed carrier such as activated carbon, and the development rate is preferably 20% or more, for example, about 20 to 50%.

When the activated carbon having an average particle size of 0.6mm is allowed to flow at LV15m/hr, the flow state is such that the degree of development is 20 to 30%. When the activated carbon having an average particle size of 0.3mm is flowed at LV 8-10 m/hr, the developing rate is 20-30%.

In the present invention, as the fluidized bed carrier, a gel-like material, a porous material, a non-porous material, or the like other than activated carbon can be used under the same conditions. For example, polyvinyl alcohol gel, polyacrylamide gel, polyurethane foam, calcium alginate gel, zeolite, plastic, and the like can also be used. When activated carbon is used as the carrier, a wide range of pollutants can be removed by the interaction between the adsorption action and the biodegradation action of activated carbon. The activated carbon is not particularly limited, and may be coconut shell carbon, coal, charcoal, or the like. The shape is preferably spherical carbon, but may be ordinary granular carbon or crushed carbon.

The average particle diameter of the carrier such as activated carbon is preferably about 0.2 to 1.2mm, particularly about 0.3 to 0.6 mm. When the average particle size is large, the LV can be set high, and when a part of the treated water is circulated in the reaction tank, the circulation amount increases, and a high load can be achieved. However, the biomass becomes less because the specific surface area becomes smaller. When the average particle size is small, the flow can be made low LV, so that the power for the pump becomes inexpensive. And the attached biomass is increased due to the large specific surface area.

The optimum particle size is determined by the concentration of wastewater, and is preferably about 0.2 to 0.4mm when the total organic carbon content (TOC) is 50 mg/L.

In the aerobic biological treatment apparatus 1 configured in this manner, raw water is introduced into the receiving chamber 7 through the raw water distribution pipe 8, and the water is introduced into the water permeable plate 3, the large-diameter particle layer 4, and the small-diameter particle layer 5 in an upward flow manner to remove Suspended Solids (SS), and then the water is introduced into the fluidized bed F of the activated carbon powder particles to which the biofilm is attached in an upward flow manner in a one-through type to carry out a biological reaction, and is taken out from the upper clarification region through the groove 10 and the outlet 11 as treated water.

An oxygen-containing gas such as air supplied from the air supply pipe 27 is introduced into the oxygen dissolving membrane module 6 in a downstream direction, and then flows out from the lower end position of the oxygen dissolving membrane module 6 through the lower header 21 and the lower manifold 24, and exhaust air is discharged to the atmosphere from the exhaust pipe 29 (or from the exhaust pipe 30 when the exhaust pipe 30 is provided). The condensed water flows out to the sump 32 through the discharge pipe 29. The oxygen-containing gas such as air may be introduced into the oxygen dissolving membrane module 6 in an upward flow manner.

Further, when the hollow fiber membrane is used as the oxygen dissolving membrane, since the cross-sectional area of the aeration portion is small, the aeration is easily inhibited, and the influence thereof is large, the above-mentioned condensed water removing mechanism is preferably used in an aerobic biological treatment apparatus in which the oxygen dissolving membrane is a hollow fiber membrane.

In the present invention, the supply oxygen amount is increased by providing a non-porous oxygen-dissolved film in a fluidized bed of a biological carrier such as activated carbon, and therefore there is no upper limit to the organic wastewater concentration of the target raw water.

Furthermore, the operation is carried out in a fluidized bed mode formed by flowing biological carriers with the average particle size of 0.2-1.2 mm under the action of the upward flow of LV 7-30 m/hr, so that the biological carriers are not in violent disturbance. Therefore, a large amount of living organisms can be stably maintained, and thus the load can be increased.

In addition, the present invention uses an oxygen dissolution membrane, so that the power for dissolving oxygen is small as compared with pre-aeration and direct aeration. In the present invention, the average particle diameter of the fluidized bed carrier is set to 0.2 to 1.2mm, so that the surface of the oxygen dissolving membrane is scraped by the carrier to prevent the adhesion and propagation of organisms, and oxygen is efficiently dissolved from the oxygen dissolving membrane into the water to be treated. Thus, a stable biological treatment can be performed by obtaining a balance between the amount of oxygen supplied from the oxygen-dissolved film and the rate of decomposition of organic substances, which is dominated by the biofilm attached to the fluidized bed carriers.

As described above, according to the present invention, it is possible to stably treat organic wastewater having a low concentration to a high concentration with a high load.

< oxygen-containing gas >

The oxygen-containing gas is air, oxygen-enriched air, pure oxygen, etc. It is desirable to remove fine particles in advance by passing the gas to be introduced through a filter.

The aeration rate is preferably about twice the equivalent of the oxygen required for the biological reaction. In contrast to the ideal amount, if the amount of ventilation is small, Biochemical Oxygen Demand (BOD) and ammonia in the treated water remain due to insufficient oxygen, and if the amount of ventilation is large, the amount of ventilation is unnecessarily large, and the pressure loss is also high, thereby impairing the economy.

The aeration pressure is preferably slightly higher than the pressure loss of the hollow fibers generated at a predetermined aeration rate.

< blower >

The blowing wind pressure of the blower is sufficient to be lower than the water pressure generated by the water depth. However, the pressure loss of the piping or the like must be increased. The piping resistance is usually about 1kPa to 2 kPa.

In general, when the water depth is 5m, a general-purpose blower having an output of about 0.55MPa at maximum is used, and when the water depth is 5m or more, a high-pressure blower is used.

In the present invention, a general-purpose blower having a pressure of 0.5MPa or less can be used even when the water depth is 5m or more, and a low-pressure blower having a pressure of 0.1MPa or less is preferably used.

The conditions of the supply pressure of the oxygen-containing gas are higher than the pressure loss of the hollow fiber membrane and the membrane is not crushed by water pressure. The flat film and spiral film have an extremely low pressure, about 5kPa or more, and a water depth pressure or less, preferably 20kPa or less, because the film pressure loss is negligible compared to the water pressure.

In the case of a hollow fiber membrane, the pressure loss varies depending on the inner diameter and length. The amount of air to be blown is 50 to 200 mL/day per square meter of the membrane, so that the amount of air is doubled if the membrane length is doubled, but the amount of air is doubled even if the membrane diameter is doubled. Thus, the pressure loss of the membrane is proportional to the membrane length and inversely proportional to the diameter.

The pressure loss value is about 3kPa to 20kPa in a hollow fiber having an inner diameter of 50 μm and a length of 2 m.

< pretreatment of raw Water and aftertreatment of biologically treated Water >

In the present invention, examples of raw water include, but are not limited to, semiconductor, liquid crystal manufacturing process drain, food factory drain, automobile manufacturing drain, mechanochemical drain, and chemical petroleum factory drain. When the raw water has a high SS concentration, it is preferable to perform pretreatment to remove SS and then supply the resulting product to the biological treatment apparatus.

In the present invention, the biologically treated water from the biological treatment apparatus may be further treated. Examples of such treatment include coagulation sedimentation treatment for removing SS or biological sludge in the treated water.

The present invention has been described in detail using specific embodiments, but it is apparent to those skilled in the art that various changes can be made without departing from the purpose and scope of the present invention.

The present application is based on japanese patent application 2018-.

Description of reference numerals

1: an aerobic biological treatment device;

2: a reaction tank;

6: an oxygen dissolving membrane module;

20. 21: a header;

22: a hollow fiber membrane;

27: a gas supply pipe;

29: a discharge piping;

30: an exhaust pipe;

31: a valve;

32: a storage tank.