JP4492896B2 - Microbial treatment method and apparatus for high concentration wastewater - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method and a device for effectively treating waste water containing a high concentration BOD component or normal hexane extract components such as waste water from swinery or food industrial without pretreatment such as dilution or removal of the solid portion. SOLUTION: The waste water containing the BOD component or the normal hexane-extract component in high concentration is treated aerobically and weak anaerobically by being passed through a high speed sprinkling filter tank 4, in which a crushed article of liparite is filled, the sprinkling treated water is aerated in an activated sludge tank to be treated aerobically and further the activation treated water is supplied to the high speed sprinkling filter tank 4 to be circulated and treated. The circulation treatment is repeated further by plural stages at need to purify the waste water.

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method and apparatus for effectively treating microorganisms containing wastewater containing BOD and normal hexane extract components at high concentrations. Furthermore, the present invention relates to a method and an apparatus for performing a decolorization treatment of treated wastewater almost completely.
[0002]
[Prior art]
Most of the wastewater containing organic (fouling) substances such as BOD and normal hexane extract components (normal hex components) are treated by the activated sludge method, lagoon method, rotating disk method, sprinkling filter bed method and the like. All of these decompose organic substances by utilizing the enzymatic action of microorganisms, and the concentration of BOD components and norhex components that can be treated is naturally limited. For example, in the case of the activated sludge method, the treatment cannot be performed when the BOD component exceeds 3000 ppm. Usually, it is processed at about 1000 to 1500 ppm at 3000 ppm or less. Therefore, such as swine sewage wastewater and food industry wastewater, the BOD component of super high concentration exceeding 3000ppm and 10,000 or tens of thousands ppm, or the oil component (norge component) exceeding 500ppm and 3000 to 10,000ppm. The wastewater containing can not be treated as it is in any treatment method, and some pretreatment is required. As this pretreatment, it is common to dilute to a treatable BOD concentration or norhex concentration, or to remove these polluted organic substances by agglomeration or pressurized flotation.
[0003]
[Problems to be solved by the invention]
However, when the wastewater is diluted, the amount of treatment increases greatly, resulting in an increase in the area of the apparatus and facility. Also, the removal in the pretreatment requires ancillary facilities, and it takes time and cost to discard or incinerate the removed organic matter. In addition, various methods such as applying high pressure have been developed. However, there is a disadvantage that it takes enormous costs to treat a large amount of waste water.
[0004]
[Means for Solving the Problems]
Therefore, the present inventor is a method for effectively treating wastewater containing high-concentration BOD components and norhexy components such as pig farm wastewater and food industry wastewater without pretreatment such as dilution or removal of organic substances (removing solids). The present invention has been completed through exploratory research.
[0005]
The gist of the present invention is a combination of a high-speed watering filter bed method and an activated sludge method, and a crushed quartz rough rock is used as a filter medium (microbe-adhering material) for a high-speed watering filter bed tank. That is, drainage from which impurities (SS component) are removed is passed through a high-speed sprinkling filter bed filled with crushed quartz rough rock to perform aerobic treatment and weak partial anaerobic treatment. Aerated water is aerated in an activated sludge tank, aerobic treatment is performed, and the activated treated water is circulated and supplied to a high-speed sprinkling filter bed tank, and a part of the activated treated water is sent to another activated sludge tank. Then, it is circulated between other high-speed sprinkling filter beds to reduce the concentration of BOD and norhex components, and this circulatory treatment is further repeated in multiple stages to purify wastewater as needed. It is.
[0006]
In general, in the case of the high-speed sprinkling filter bed method, it is said that clogging occurs when the BOD volumetric load per 1 m ^{3 of} the filter medium exceeds 1.5 to ³ Kg. Further, in the activated sludge method, when the BOD volume load exceeds 0.3 to 0.6 kg, the sludge does not settle and good treatment cannot be performed. On the other hand, in the case of the present invention, the BOD volume load per 1 m ^{3 of} the filter medium can be processed up to about 1.5 to 15 kg. This is because the surface of the filter medium is fine in the form of a honeycomb and excellent in microbial survival, and organic substances are effectively decomposed by various biota ranging from microorganisms to protozoa that prey on them. In this step, aerobic treatment is mainly performed, but a weak anaerobic treatment is also performed on the lower side of the biofilm, thereby reducing the molecular weight of the polymer substance and reducing the BOD component and the norhex component. And the waste water which passed the filter medium falls to the activated sludge tank in the lower side, an aerobic microorganism process is performed in this activated sludge tank, and the oxidation of organic substance advances further. The wastewater from the activated sludge tank is pumped up to the sprinkling filter bed by a certain amount and sequentially circulated.
[0007]
Next, a part of the wastewater in the activated sludge tank is sent to other activated sludge tanks and circulated between other high-speed watering filter beds to further reduce the concentration of BOD and norhex components. Let Therefore, in the case of the present invention, there is no problem even if the oxidation treatment is delayed because the BOD concentration or the concentration of the norhex component in the first activated sludge tank is too high. If necessary, this circulation process is repeated a plurality of stages. In addition, the capacity | capacitance of each tank and the quantity of a filter medium are designed by the BOD density | concentration of a wastewater to process, a norhex ingredient concentration, and the amount of drainage. The circulation treatment may be about 10 to 24 hours if the BOD concentration is about 1000 ppm to several thousand ppm, and if it is about 10,000 to 20,000 ppm, 3 to 4 days, about 60,000 ppm of radish drainage. If it is a wastewater from dairy juice (daikon radish to be disposed of) or 5-80,000 ppm, circulate for 6-8 days. This circulation processing time is the total time in the case of a multi-stage process (a plurality of sets of high-speed watering filter bed tanks and activated sludge tanks). In general, two or more stages are performed, and if the BOD concentration is high, three to four stages are performed. And if processing takes days, the capacity | capacitance of an activated sludge tank will become correspondingly large, but since the capacity | capacitance is the sum total of the number of stages, the capacity | capacitance of one activated sludge tank is very small compared with the case where it dilutes. There is an advantage of being a thing.
[0008]
The quartz rough rock used for the filter medium in the present invention is a kind of acidic volcanic rock, rich in silica, and when in contact with water, a small amount of silicic acid and magnesium are leached to form silicate. Moreover, it is a porous material having countless cavities penetrating in a honeycomb shape and has a large surface area, and is ideal as a microorganism savory house. Therefore, in the case of a high-speed sprinkling filter bed filled with this crushed product as a filter medium, the food chain is vigorously caused by biological activity in the filter medium, and even if wastewater with a high concentration of BOD or norhex component is introduced, the special decomposition that is alive The organisms generated according to the bacteria and the place are treated.
[0009]
Next, the microorganism of the present invention, that is, the above-described special degrading bacterium will be described. In general, the microorganisms deposited for treatment depend on the group of microorganisms that grow naturally. The same applies to the present invention, but in addition, certain microorganisms adapted to the waste water to be treated, in particular, Bacillus subtilis, Pseudomonas sp., Mucro sp Rhizopus sp, Ascomycetes (Aspergillus sp Penicillum sp), infectious bacteria (Fusarium sp Geotricum sp Tricomoderma sp) and other bacterial groups combined with the bacteria are deposited on the filter media and, if necessary, added to the treatment system. Increase. However, it takes time to adapt from scratch, so in advance cultivate a group of microorganisms with a high degradability according to the type of organic matter such as oil, starch, protein, etc., analyze the wastewater to be treated and analyze it The microbial groups are combined according to the contained components, and the combined microbial groups are deposited on the filter medium. In this way, good microbial treatment can be performed from the beginning of the treatment.
[0010]
Subsequently, in the method of the present invention, the amount of drainage, the concentration of BOD components in the drainage, and the required capacity of each treatment tank will be described. For example, in the case of wastewater with a concentration of 10,000 ppm of BOD component and norhex component excluding solid content (100 m ³ per day), the amount of BOD / norhex component to be treated is 1000 kg / day. If this process is performed in 4 days, the total amount of drainage is 100 × 4 = 400 m ³ . When this is treated with a set of three-stage high-speed sprinkling filter bed tank and activated sludge tank, the capacity of each tank is 150 m ³ . Further, if the BOD load per 1 m ³ of the filter medium in the high-speed sprinkling filter bed tank is 10 kg, the filter medium needs 1000 ÷ 10 = 100 m ³ , for example, 50 m ³ for the first high-speed sprinkling filter bed tank, It is good to fill the high-speed sprinkling filter tank with 30 m ^{3 at a} time. If the amount of the filter medium is increased, the BOD load per 1 m ^{3 of} the filter medium can be reduced, and more relaxed processing can be performed. In the case of the present invention, the BOD load per 1 m ^{3 of} the filter medium can be up to about 1.5 to 15 kg.
[0011]
This filter medium load may be increased when the BOD discharge standard of the treated water is high (the standard is sweet), but the load cannot be increased when the discharge standard is as severe as 20 to 30 ppm. Incidentally, watering per filter medium 1 m ³ at our fast watering filter bed vessel, the chelating is completed by circulating 30 m ³ / day ~40m ³ / day. In the case of high-concentration wastewater, chelation can be promoted by circulating wastewater of 50 m ³ / day per 1 m ³ of filter medium in the previous stage. In the latter part, 40 m ³ / day is sufficient. When circulating the effluent of the filter medium 1 m ³ per 50 m ³ / day, to the drainage ^{100m 3 / m 3 × 50m 3} / day ÷ 24 hours ÷ 60 minutes ≒ 3.5 m ³ / min of the amount may be pumped up Become.
[0012]
If wastewater of the same concentration and amount is treated by the conventional activated sludge method, if it is treated at 1000 ppm, a 10-fold dilution is required. And this in treatment with 2-day activated sludge tank of ^{100m 3 × 10 × 2 = 2000m} 3 is required. On the other hand, in the case of the present invention, a total activated sludge tank of 400 m ³ (450 m ^{3 in} excess) is sufficient, and a significant reduction in installation area can be realized.
[0013]
Thus, according to the biological treatment method of the present invention, wastewater containing high-concentration BOD components and norheke components, such as swine wastewater and food industry wastewater, can be treated in a shorter time and with a smaller device to meet wastewater standards. The only problem that is difficult to solve is the problem of coloring. The coloring component is said to be a humic substance or a carbon compound and is a component of BOD or COD. However, there are cases where the degree of coloring is severe even within the range of the wastewater standard. The degree of coloring decreases when the treated wastewater is passed through an anaerobic tank or a weak anaerobic tank again, but cannot be completely decolorized. If activated carbon is used, complete decolorization is possible, but it causes a significant cost increase.
[0014]
The following experimental results have been reported for the coloration of wastewater that has undergone biological treatment. That is, the organic matter in the barn effluent is roughly divided into components having a molecular weight of 3000 or more with a low TOC but high chromaticity and components having a molecular weight of 3000 to 100 with a low chromaticity but high TOC. In the biological treatment (aerobic treatment), the latter can be decomposed, but the former is difficult to decompose. And although the former density | concentration did not increase by aerobic treatment, the phenomenon which chromaticity increased was seen. This is presumably because a substance having a molecular weight of 3000 or more has an azo group, and the degree of color development was increased in an aerobic atmosphere (water treatment technology, Vol. 40 No. 12 1999).
[0015]
This is consistent with our experience. And also in the above-mentioned processing apparatus, the chromaticity of treated water is low by the treatment in the denitrification / reduction tank (13). However, although the coffee color is still brownish, it is far from colorless.
[0016]
Accordingly, the present inventors have further studied on the decolorization of the colored treated water subjected to the above-mentioned treatment, and as a result, have come up with the adoption of electrolysis. That is, a substance having a molecular weight of 3000 that cannot be decomposed by the aerobic biological treatment was separated and decomposed by electrolysis. However, since these substances are very difficult to separate and decompose, it is necessary to increase the voltage. For this reason, it has been found that the metal used for ordinary electrolysis has a very high temperature including platinum and is difficult to use. In addition, various metals and organic substances remain in the treated waste water, and aluminum and iron are not worn out and dirty due to corrosion, and stainless steel can be used for the anode because chromium and other metals are eluted. Can not. In the case of platinum, neither the anode nor the cathode has these drawbacks, but a high voltage is applied, so the heat is intense and the cost is high, so it cannot be used for wastewater treatment.
[0017]
Therefore, when a carbon iron rod sintered with carbon and iron is used for the anode and a stainless steel rod is used for the cathode, even when a current of 10 to 20 V, 15 to 25 A (experimental machine) is passed, the heat generation is about 50 ° C., and There was no elution from the electrode. In addition, since no excessive current flows and consumption of electricity is reduced, and separation and decomposition of organic substances can be performed with certainty, the treated water is almost colorless and the decolorization is performed completely. In addition, when it is this electric current value, the water temperature will also be 70 degreeC or more in platinum. Moreover, in the case of wastewater treatment by conventional electrolysis, chemicals are injected for the purpose of improving the electrical conductivity and adjusting the pH, but in the case of the present invention they are not necessary at all. . This seems to be because the electrode, voltage and other conditions are consistent with the wastewater treatment. Note that the current value in an actual apparatus is 50 to 1000 A, depending on the capacity of the apparatus. The electrolysis treatment time is about 1 hour when the color of the drainage is light brown, and about 2 hours when the color is dark like coffee.
[0018]
However, when electrolysis is performed for a long time, metal deposits are observed on the electrode, particularly the cathode. In such a case, the electrode is generally reversed so that the metal adhering to the cathode is peeled off. However, in the case of platinum or other metal electrodes, there is no problem even if it is reversed for a long time of 1 hour or more, but in the case of the carbon iron electrode, when the electrode is reversed, the structure of the sintered body is damaged by the shock. However, there is a risk of becoming tattered. Therefore, in the present invention, it is necessary to perform this reversal for an extremely short time of about 1 to 5 minutes and to repeat this several times a day. If the cathode is not sufficiently cleaned because the reversal time is short, cleaning is promoted by applying ultrasonic waves. By the way, although it is a short time, stainless steel temporarily becomes an anode by reversal, and as a result, metals such as chromium may be eluted from the stainless steel. Therefore, it is preferable to use titanium or tantalum instead of stainless steel. Titanium is the most preferable because it can be obtained at a relatively low cost.
[0019]
As described above, when the water biologically treated by the method of the present invention is further electrolyzed with carbon iron as an anode and stainless steel or titanium or tantalum as a cathode, an organic substance having a molecular weight of 3000 or more is separated and decomposed and decolorized. Along with the treatment, ammonia is converted into nitrogen gas, and phosphorus is also converted into a phosphoric acid compound to remove most of it. More preferably, the treatment liquid is heated to around 50 ° C. by the heat generated during electrolysis, and the treatment lasts for about 1 to 2 hours, so that many effects such as the ability to kill viruses and bacteria are possible. It is obtained. The electrolysis of the method of the present invention is extremely excellent in decoloring properties. The biological treatment of the present invention has an aeration time as short as about 1/3 compared to a normal biological treatment method (about 30 days are about 10 days). Therefore, it is considered that an increase in color development due to oxidation of a substance having a molecular weight of 3000 or more is small.
[0020]
DETAILED DESCRIPTION OF THE INVENTION
(Embodiment 1)
FIG. 1 shows an example of a flowchart in the case of treating food factory effluent based on the method of the present invention. This wastewater is wastewater from a Sakai factory. The raw water has a BOD concentration of 2000 to 15000 ppm (average 4500 ppm), a norhexane component concentration of 1500 to 25000 ppm (average 6000 ppm), and a daily drainage amount of 45 m ³ / day. It passes through the denitrification / reduction tank 13 to the precipitation tank 14 and is discharged.
[0021]
The drainage standards for river discharge are BOD of 120 ppm or less and norhex component of 30 ppm or less. Therefore, the drainage standard formula of this factory is as follows.
BOD: 45 m ³ / day × 4500 ppm × 0.003 = 202.5 kg / BOD / day oil content: 45 m ³ / day × 6000 ppm × 0.003 = 270 kg / oil content / day, In this example, the final treated BOD was 30 ppm or less, norhex component was 5 ppm or less.
[0022]
That is, 202.5 kg / BOD · day, 270 kg / oil / day are processed. This process was performed by the apparatus shown in FIG. In FIG. 1, the factory wastewater collected in the raw water tank 1 is solid-liquid separated by the screen device 2 and sent to the adjustment tank 3. The waste water sent quantitatively from the adjustment tank 3 is a first circulation tank 6 that combines a high-speed watering filter bed tank 4 and an activated sludge tank 5, and also a high-speed watering filter bed tank 7 and an activated sludge tank 8. It processes sequentially in the 3rd circulation tank 12 which combined the 2nd circulation tank 9, the high-speed watering filter bed tank 10, and the activated sludge tank 11. FIG. The treated water is sent to the denitrification tank / reduction tank 13 and further separated from the sludge in the sedimentation tank 14 and discharged into the river as treated water. Reference numeral 15 denotes an effective bacteria culture tank, in which treated water, other nutrient sources, and effective bacteria are added and cultured, and added to each high-speed sprinkling filter bed as appropriate. Here, the effective bacteria means that a group of microorganisms having a high decomposability according to the type of organic matter such as oil, starch, protein, etc. is cultured in advance, the wastewater to be treated is analyzed, and the components contained therein are analyzed. It is a combination of microorganisms, and is a group of microorganisms combining bacteria such as the genus Pseudomonas and Bacillus as the microorganism group. In this way, good microbial treatment can be performed from the beginning of the treatment. If this fungal group is activated in a balanced manner with other naturally occurring fungal groups, this addition may be stopped.
[0023]
The capacity of the adjustment tank 3 is 10 hours a day (the treatment is performed continuously for 24 hours), 45 m ³ / day × (24−10) ÷ 24 = 26 m ³ . Again, aeration processing is performed. The amount of air is 3.5 m ³ / H per 1 m ^{3 of} water. The general air amount is about 1.8 to 2.2 m ³ / H, but in the case of the present invention, it is due to the high concentration waste water. Further, if the amount of water at that time is 75% of the tank, 26 m ³ × 0.75 = 19.5 m ^{3 is} required. The required amount of air is 19.5 m ³ × 3.5 m ³ /H≈0.14 m ³ / min. In the adjustment tank 3, the oil content cannot be decomposed, and the BOD is reduced by about 15 to 20%. If the BOD removal rate is 15%, then 202.5 kg / day × 15% = 172.2 kg / day.
[0024]
The capacity of the first and second activated sludge tanks 5 and 8 forming the first and second circulation tanks 6 and 9 is 45 m ³ × 2 days = 90 m ³ , as a total stay of 2 days (contact). The amount of the activated sludge tank 3 is 45 × 2/3 = 30 m ³ as 2 / 3-day retention. The amount of air in each activated sludge tank is 2.5 in the front tank, 1.8 in the rear tank, and 2 m ³ / H on average per 1 m ^{3 of} water. Therefore, (90 m ³ +30 m ³ ) × 2 m ³ ÷ 60 minutes = 4 m ³ / min in ^three tanks.
[0025]
The amount of filter medium 41 to be put in each high-speed sprinkling filter bed tank 4, 7, 10 is 5 kg / m ³ per 1 m ^{3 of} filter medium load for river discharge, 202.5 kg / day ÷ 5 kg / m ³ = 40.5 m ^{Use 3} . When the amount of water sprayed is 40 m ³ / day per 1 m ^{3 of} filter medium, 40.5 m ³ × 40 m ³ /day≈1.125 m ³ / min. In addition, the crushed product of the quartz rough surface rock of the size of fist size or about 3 times that was used for the filter medium. Reference numeral 42 is a water spray pipe, and reference numeral 43 is a diffuser pipe disposed in each activated sludge tank 5, 8, 11.
[0026]
The removal rate in the circulation tank is 172.2 kg / day × 30% = 120.5 kg / BOD · day, 270 kg / day × 50% = 135 kg as BOD 30% and norhex component 50% in the first circulation tank 6. / Nor hex ingredient / day. Similarly, in the second circulation tank 9, the removal rate is 60% in BOD, 120.5 kg / day × 60% = 48.2 kg / day, the norhex component is 85%, 135 kg / day × 85% = 2.25 kg. / Day. In the third circulation tank 12, the removal rate is 98% in BOD, 48.2 kg / day × 98% = 0.96 kg / day, the norhex component is 99%, and 20.25 kg / day × 99% = 0.20 kg. / Day.
[0027]
Capacity of denitrification combined reduction vessel 13, when 3 hours residence time, the 45 m ³ / day ^{÷÷ 24 ÷ 3 = 5.6 m 3} . Somewhat and 6m ³ as large. The amount of air in this tank may be about stirring. The removal rate in the denitrification tank / reduction tank 13 is about 5% in terms of BOD. Finally, as a result of the processing in the apparatus of the present invention, the BOD is 0.96 × 0.5% = 0.91 kg / day.
[0028]
(Embodiment 2)
Pig farm wastewater (10 m ³ / day) having a BOD of 6000 to 20,000 ppm was treated using the same apparatus as in the above example. In this embodiment, the water treated in the first circulation tank 6 and the second circulation tank 9 as the first stage is stored in the settling tank 14, and the wrinkled water is further treated in the two circulation tanks as the second stage. Next, the denitrification / reduction tank 13 and the precipitation tank 14 are drained. As a result, the BOD became 1100-1500 after the second-stage circulation tank treatment, and when this was precipitated and separated, a BOD of 15-35 was obtained, which had a beautiful numerical value that could be discharged as it was.
[0029]
(Embodiment 3)
When the treated wastewater obtained in Example 2 was further electrolytically treated with the electrolyzer 16 shown in FIGS. 2 and 3, surprisingly, treated water having almost no coloration and extremely high transparency was obtained. Moreover, the BOD ability of this treated water was 3 to 5 ppm. This is more beautiful than general river water (several to tens of ppm). The electrolysis apparatus 16 is a laboratory model, and a carbon iron rod 18 having a diameter of 2.5 cm and a length of 20 cm as an anode and a cathode inside a plastic tank 17 having a width of 16 cm, a length of 100 cm, and a depth of 3 cm. As shown in FIG. 2, stainless steel bars 19 having the same dimensions are alternately arranged. Reference numeral 18a denotes an anode rod terminal, 19a denotes a cathode cord mounting screw hole, and 20 denotes an insulating rubber plate. The rods 18 and 19 are inserted and supported in through holes provided in the lower frame 21 and the upper frame 22 with an interval of about 5 mm. Further, an aeration air outlet 23 is provided in the lower part of the plastic tank 17, and an inlet 25 of the drainage 24 and an outlet 27 of the electrolyzed drainage 26 are provided in the upper part. The processing conditions were 13 to 18 V, 15 to 25 A, and circulation processing was performed for about 1 hour.
[0030]
【The invention's effect】
As described in detail above, the method of the present invention circulates waste water containing BOD and norhex component at a high concentration between a high-speed watering filter bed filled with crushed quartz rough rock and an activated sludge tank. The concentration of these organic substances is reduced. In addition, the bacteria mixed with the wastewater to be treated is alive on the filler of the high-speed sprinkling filter.
[0031]
Therefore, the BOD volume load is orders of magnitude greater than the high-speed sprinkling filter bed method in which clogging occurs when the BOD volume load becomes high, such as pig farm wastewater and food wastewater, and the activated sludge method in which sludge does not settle and good treatment is not performed. Even in wastewater, the oxidation of organic matter proceeds with time, and the molecular weight of the polymer substance is reduced and the BOD component and the norhex component are reduced.
[0032]
In addition, the apparatus of the present invention incorporates a high-speed watering filter bed filled with a crushed quartz rough rock between the raw water tank and the settling tank, and an aeration apparatus disposed below the high-speed watering filter bed tank. A plurality of treatment tanks each including an activated sludge tank are arranged. Accordingly, there is a feature that the waste water can be effectively treated even if the installation area is small.
[0033]
Furthermore, when the electrolysis treatment of the present invention is carried out, there is no corrosion of the electrode and the heat generation is small, and there is no chemical injection as in the conventional case, and the colored biologically treated water is almost colorless and decolorized to the present time. In addition, BOD, oil, nitrogen and phosphorus are significantly removed, and the effect of almost completely killing viruses and bacteria is obtained.
[Brief description of the drawings]
FIG. 1 is a flowchart showing an example of a method of the present invention.
FIG. 2 is a plan view showing an example of the electrolysis apparatus of the present invention.
FIG. 3 is a longitudinal sectional view showing an example of the electrolysis apparatus of the present invention.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 1 Raw water tank 2 Screen apparatus 3 Adjustment tank 4 High-speed sprinkling filter bed tank 41 Filter medium 42 Sprinkling pipe 43 Aeration pipe 5 Activated sludge tank 6 First circulation tank 7 High-speed sprinkling filter bed tank 8 Activated sludge tank 9 Second circulation tank 10 High-speed sprinkling filter bed 11 Activated sludge tank 12 Third circulation tank 13 Denitrification / reduction tank 14 Sedimentation tank 15 Effective bacteria culture tank 16 Electrolytic device 17 Plastic tank 18 Carbon iron bar 18a Anode bar terminal 19 Stainless bar 19a For cathode Cord mounting screw hole 20 Insulating rubber plate 21 Lower frame 22 Upper frame 23 Aeration air outlet 24 Drain 25 Inlet 26 Electrolyzed drain 27 Outlet

Claims (3)

The wastewater containing BOD and normal hexane extract components at high concentration is passed through a high-speed sprinkling filter bed filled with crushed quartz rough rock as a filter medium after removing contaminants for aerobic treatment and weak anaerobic treatment. The aerated water is aerated in an activated sludge tank for aerobic treatment, and the activated treated water is circulated in a high-speed sprinkling filter bed, and a part of the activated treated water is subjected to other activities. Liquid is sent to the sludge tank and circulated between other high-speed sprinkling filter bed tanks to reduce the concentration of BOD and normal hexane extract components, and this circulation treatment is repeated in multiple stages as necessary to purify wastewater. The treatment water treated with microorganisms is subjected to decolorization treatment by introducing it into an electrolysis treatment tank using a carbon iron rod sintered with carbon and iron as an anode and stainless steel, titanium or tantalum rod as a cathode. Takano Microbial treatment method of waste water.   Bacteria mixed with Pseudomonas spp. The microbial treatment method of high concentration waste water according to claim 1, wherein the fungus group is introduced into a high-speed sprinkling filter bed as needed. Between the raw water tank that receives wastewater containing BOD and normal hexane extract components at high concentrations, the adjustment tank that quantitatively feeds the raw water excluding impurities to the treatment tank, and the precipitation tank that receives the water treated in the treatment tank, A plurality of treatment tanks, one set consisting of a high-speed sprinkling filter bed filled with crushed rough rocks, and an activated sludge tank installed under the high-speed sprinkling filter bed tank and incorporating an aeration device, are arranged for further processing. An anaerobic denitrification tank is provided next to the tank, and an electrolytic treatment tank is provided next to the anaerobic denitrification tank, with a carbon iron rod sintered with carbon and iron as an anode and a stainless steel, titanium or tantalum rod as a cathode. A microbial treatment apparatus for high-concentration wastewater.

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