KR200187972Y1 - The processeing equipment for waste water and net barrel supplying device - Google Patents

Abstract

The present invention aims to provide a rotary carrier filling device that minimizes the amount of sludge and can simultaneously process nitrogen and phosphorus as well as organic matter. Screen sedimentation tank, flow control tank, phosphorus discharge tank, anoxic tank , The first and second reaction tanks, the return pump tank, and the final settling tank are installed in order, and the return pump tank is provided with a return line for returning the sludge to the anoxic tank, and the supernatant of the final settling tank is discharged to the disinfection discharge tank through the defoaming tank. Some of the supernatant water of the tank is sent to the first and second reactors, and the sludge of the final settling tank is sent to the dehydration facility through the sludge concentration tank and the concentrated sludge storage tank, and the phosphorus discharge tank, the anoxic tank, and the first and second reaction tanks are It has a screen to guide the influent sewage in the direction of the center and installs a rotary tin filling device filled with contact material inside. This prevents excessive sludge deposition in the anaerobic phosphorus discharge tank and the anoxic tank and helps the release and denitrification of phosphorus. By ingesting a large amount of organic matter to promote nitrification and intake of phosphorus, it is configured to increase the removal efficiency of organic matter and of course nitrogen and phosphorus.

Description

The processeing equipment for waste water and net barrel supplying device

The present invention relates to a rotary carrier filling device to compensate for the shortcomings of standard activated sludge treatment apparatus, catalytic oxidation treatment apparatus and various deformation treatment apparatus in sewage treatment process, and in particular, adding a rotary carrier filling apparatus, anaerobic tank and anoxic tank condition. The present invention relates to a rotary carrier filling apparatus which minimizes the amount of sludge generated by eliminating the sludge conveying process, and simultaneously handles nitrogen and phosphorus as well as organic matter.

The existing standard activated sludge treatment is the most common sewage treatment. This method returns 20 ~ 40% of activated sludge from the final settling tank to the aeration tank, mixes the influent sewage and activated sludge, separates the sludge from the final settling tank and discharges the supernatant. The MLSS is 1,500 ~ 3000, BOD. The load is about 0.2 to 0.4 Kg / m ³ .

The characteristics of this method are that the activated sludge with good sedimentation is obtained and its function is normal, but the adjustment of MLSS corresponding to the BOD load and the adsorption and oxidation balance depending on the quality and aeration time of the activated sludge, the control of sludge and air supply Professional management is required, it is possible to operate economically in large-scale facilities of the facility, it is unstable in fluctuation of load of influent and sludge occurs, which requires a lot of maintenance costs.

The catalytic oxidation method compensates for the disadvantages of the activated sludge process by filling contact materials in the aeration tank to remove the organic matter in the sewage by the decomposition of microorganisms while circulating contact with the biofilm formed on the surface of the carrier. High concentration of microorganism of ~ 50,000mg / ℓ can be attached to the contact material, so it is strong against the influent organic matter and hydraulic load fluctuation, and it does not need the conveying sludge, so it is easy to manage and produce less sludge but uniformly agitate the media in the aeration tank. It is pointed out that it is difficult to set the condition, that there is a risk of dead space, and that the load condition is limited because of the high risk of closing the medium at high loads, so that it is applicable to only small sewage treatment facilities.

Standard activated sludge treatment and catalytic oxidation treatment are secondary treatment facilities, which mainly remove organic matter. Recently, as the phenomenon of eutrophication becomes a social problem, a new water treatment method for removing nitrogen and phosphorus has been proposed. Representative biological nitrogen and phosphorus simultaneous removal methods include A ² / O, Barden pho, VIP. The outline and problems of these are as follows.

In Figure 1, the A ² / O method is to remove the nitrogen oxide and phosphorus at the same time by installing an anaerobic tank between the anaerobic tank and aerobic tank in the existing A / O method, the F / M ratio is 0.15 ~ 0.25kg BOD / kg MLVSS It is day and SRT (solid residence time) is 4-27 days. The hydraulic retention time (HRT) is 0.5-1.5 hours for the anaerobic section, 0.5-1.0 hours for the oxygen depletion section and 3.5-6.0 hours for the aerobic section, and the average MLSS of the aeration tank is maintained at 3,000-5,000 mg / l. On the other hand, the A ² / O process can reduce the content of nitrogen oxide (NO ₃ ) of the return sludge can reduce the effect of nitrogen oxide in the dephosphorization process. The denitrification cycle from the aerobic tank usually reaches 100-300% of the influent, and the phosphorus removal rate is lower than that of the A / O process, but can remove 40-70% of nitrogen. However, even in the A ² / O process, denitrification can be controlled by denitrification return rate, but it is not perfect. This is because NO _x remains in the conveying sludge. This is returned to the anaerobic tank, which ensures the growth of phosphorus-free microorganisms, which affects the removal of phosphorus. In order to process phosphorus highly, sand filtration or chemical treatment facilities should be additionally installed and it is difficult to operate in winter because it is greatly affected by temperature.

In Figure 2, the 5-stage Badenpo process is designed to increase the removal efficiency of nitrogen at low organic loads, and is to remove the phosphorus by adding an anaerobic tank to the existing Badenpo process, the treatment process is influent and return The sludge is mixed, the fermentation reaction and phosphorus release proceed in the anaerobic tank, and about 70% of the nitrogen oxides generated in the first denitrification tank together with the mixed liquid returned inside are removed together with the soluble BOD. Next, BOD, ammonia and phosphorus are removed in the aerobic tank, and the denitrification reaction takes place using the carbon source generated by decomposing microorganisms in the second denitrification tank. The second aerobic bath prevents the release of phosphorus from anaerobic microorganisms in the settling tank. The F / M ratio in this process is 0.1 to 0.2 kg BOD / kg MLVSS days, and the SRT (solid residence time) is operated for 10 to 40 days. The MLSS of the aeration tank is maintained at an average of 2,000 to 4,000 mg / l, and it is known that the phosphorus can be discharged to 3 mg / l or less, and has a removal efficiency of about 80% or more of nitrogen and about 60% of phosphorus.

However, in order to treat phosphorus highly in this process, additional facilities have to be installed, and the site of the facility is excessive compared to the A ² / O method. There is a task ahead for us to apply to other countries with different icons.

VIP process of Figure 3 is proposed to promote the high efficiency of operation compared to the UCT process. The UCT process was designed for 10-30 days of microbial retention time, while the VIP process was designed for 5-10 days of microbial retention time. The VIP process focuses on increasing the amount of active microorganisms to increase phosphorus removal efficiency and reduce reactor capacity. The VIP process is also characterized by two or more complete mixing tanks in series for each anaerobic, anaerobic and aerobic reactor to take advantage of the reactor's plug-flow. According to this method, the residual amount of organic matter in the first reactor in the aerobic mixing tank can be increased to increase the phosphorus removal efficiency. However, the VIP process has a disadvantage in that the removal efficiency of nitrogen is sharply lowered than other processes, especially in the cold zone.

Such a conventional sewage treatment method is a modified method of activated sludge method, and there is a problem in applying it widely because of the limitations of sewage properties and local conditions, and huge installation and maintenance expenses. Most existing sewage treatment plants use the standard activated sludge process. As it is an organic material treatment method installed before the discharge water quality regulation of nitrogen and phosphorus, it is urgent to expand additional facilities for nitrogen and phosphorus treatment in the future. Nitrogen-phosphorus simultaneous removal facilities such as A ² / O, Badenpo and VIP have many problems in terms of cost and maintenance.

The present invention is intended to solve the problems of the existing sewage treatment method is suitable for small and medium-sized sewage treatment plant, can be easily installed in the existing sewage treatment plant.

The present invention is to install a plurality of porous plates side by side at predetermined intervals in the rotary shaft in the phosphorus discharge tank and the anoxic tank, the first reaction tank and the second reaction tank of the sewage treatment facility installed to remove nitrogen and phosphorus in the sewage at the same time. Carrier with a partition that divides the space into radial spaces and divides the space approximately divided into concentric circles, and a screen that guides the sewage flowed into the outer circumference in the direction of the center of rotation. Provides a rotary tin charging device installed charging device.

1 is a sewage treatment process diagram of the A ² / O method

2 is a sewage treatment process chart of the 5-stage Badenpo process

3 is a sewage treatment process diagram of the VIP method

4 is a process chart of the sewage using the present invention

5 is a partial cutaway front view of a rotary carrier filling device

6 is a plan view of a rotary carrier filling device

7 is a front view of an existing contact member

8 is a front view of a contact member

Explanation of Major Parts in Drawing>

1 screen and sedimentation tank 2 flow adjustment tank

3: phosphorus discharge tank 4: anoxic tank

5: first reactor 6: second reactor

7: transfer pump tank 8: final settling tank

9: defoaming tank 10: disinfection discharge tank

11: sludge harvesting tank 12: concentrated sludge storage tank

13: dehydration facility 15: rotary carrier charging device

152: perforated plate 153: interval

154: compartment 155,155b: contact material

156,157: screen

Next, the present invention will be described in detail with reference to the accompanying drawings of FIG. 4.

In FIG. 4, the inflow sewage removes sand or contaminants in the inflow water while passing through the screen immersion tank 1 in which the screen 1a is installed, thereby preventing the functioning of subsequent processing units. The flow rate adjusting tank 2 is installed after the screen immersion tank 1. The influent sewage remains in the flow regulating tank 2 for a certain time in order to equalize the flow rate and the properties to stabilize the treatment efficiency, and then is transferred to the anaerobic phosphorus discharge tank 3 using the flow regulating pump 2a. The oxygen-free tank 4 is provided following the phosphorus discharge tank 3, and the 1st, 2nd reaction tanks 5 and 6 are provided in the back of the oxygen-free tank 4, respectively. In these reactors (5, 6), sewage treatment by the aerobic biofilm method is carried out, and it is operated at a low speed to prevent anaerobicization due to deposition or excessive adhesion of the biofilm and to remove and wash sludge. In the phosphorus discharge tank 3, the oxygen-free tank 4, and the first and second reaction tanks 5 and 6, a rotary carrier filling device 15 is provided and the phosphorus discharge tank 3 and the oxygen-free tank are desorbed when necessary. The air supply diffuser 16 is provided in the lower part of (4) and the 1st, 2nd reaction tanks 5 and 6 inside. The air supply source to the diffuser 16 of the 1st, 2nd reaction tanks 5 and 6 as an aerobic tank is a blower. In addition to the acid pipes 16 of the first and second reactors 5 and 6, the acid pipes 17 are installed on the side to prevent anaerobicization, so that the DO concentration required for intake of phosphorus is 2 mg / l or more, thereby improving phosphorus removal efficiency. Increase

The conveyance tank 7 is provided in the back of the 2nd reaction tank 6. A pump 7a is installed in the transfer tank 7 to return the treated sewage that has passed through the second reactor 6 to the anoxic tank 4 to promote denitrification.

In the first and second reaction tanks 5 and 6, various microbial species are concentrated in the contact material 155 without a dead space due to proper agitation in an aerobic state, so that organic matters are easily decomposed and phosphorus discharge tank 3 is used. Ingestion of phosphorus released from the process proceeds and after the nitrification reaction is internally circulated to the anoxic tank (4) to maintain the optimal DO concentration so as not to become anaerobic and denitrification reaction.

The final settling tank 8 is installed following the conveying tank 7. The treatment sewage flowing into the final settling tank 8 flows into the center well 8a and flows radially, and the sludge is settled and transferred to the sludge concentration tank 11 by the sludge pump 8a. The supernatant water is transferred to the defoaming tank 9 through the weir.

The defoaming tank (9) is provided with a defoaming pump (9a) in order to remove bubbles generated during the aeration process in the first and second reaction tanks (5,6) in an emergency. The defoaming pump 9a sprays the supernatant water in the defoaming water tank 9 onto the reaction tanks 5 and 6 to remove bubbles. After passing through the defoaming water tank 9, the defoaming and discharge tanks 10 of the sewerage system are discharged. The final spill. The sludge discharged from the final settling tank 8 is dewatered (BO) by the sludge pump 11a, and the supernatant is returned to the flow adjusting tank 2 for reprocessing. And the sludge of the concentrated sludge storage tank 12 is sent to the dehydration facility 13 by the pump 12a, dehydrated, and discarded.

5 and 6, the rotary carrier filling device 15 is provided with a plurality of porous plates 152 having the same diameter on the rotary shaft 151 at predetermined intervals, and the rotary shaft (between the porous plates 152 of each layer) The space | interval 153 is radially installed centering around 151, and the contact material 155 is charged for each compartment 154 divided by the space | interval 153. As shown to FIG. At the same time, the screens 156 and 157 are provided at points halfway around the circumference of the porous plate 152 and its radius. All screens 156 and 157 are inclined in a direction that attracts the surrounding sewage in the direction of the center, with the preferred inclination of the screens 156 and 157 being approximately 45 ° with respect to the tangent line. If the slope is too large, the resistance to the sewage is large, and the load is applied to the motor. If the slope is too small, the induction function in the center direction is weak, and the contact effect with the contact member 155 is low.

The contact member 155 is a waste synthetic resin, and replaces the conventional C-type contact member 155a of FIG. 7 with the corrugated contact member 155b of FIG. 8. The corrugated contact materials 155b are arranged in a vertical row, but it is advantageous to ensure sufficient sewage distribution space between the contact materials by preventing adjacent contact materials from sticking together. In particular, the corrugated contact material 155b is suitable for minimizing the occurrence of the catchment area. The arrangement direction of the corrugated contact material 155b is the same as that of the screens 156 and 157. It does not interfere with the sewage induced in the center direction, and smoothly performs the original function of the contact material.

The rotary carrier filling device 15 in the anaerobic tank phosphorus discharge tank 3 and the anoxic tank 4 creates an optimal environment in which microorganisms can grow under the influence of the contact material 155 in the device, It prevents excessive sludge accumulation and contributes to increase phosphorus release and denitrification efficiency.

The optimum operating conditions and the treatment results of sewage treatment using the present invention are as follows.

Treatment Example 1. Domestic Sewage Treatment Plant (1,200t / day)-Contact Oxidation Method

Table 1. Analysis of treatment results of influent and effluent

Metric Before treatment After treatment Processing efficiency (%) BOD (mg / l) CODSS (mg / l) T-N (mg / l) T-P (mg / l) 12681129.0456 5.666.515.303.7 9592956638

Treatment Example 2 Pilot Experiment of Sewage Treatment Plant

Table 2. Component Analysis of Influent Water (Unit: mg / ℓ)

division Analysis item CODcr CODmn BOD SS T-N T-P Primary 421 63 308 58 36 4.9 Secondary 420 57 304 236 40.2 3.3 3rd 420 60 292 134 34.2 4.1 Average 420 60 301 142 36.80 4.10

Table 2-1. How to measure

Item How to measure Analyzers and Instruments Temperature Direct measurement DO meter pH Potentiometric method pH meter DO Electrode method DO meter BOD Winkler-Sodium Azide Modification BOD incubator CODmn Water pollution process test method COD measuring device CODcr Standard Method Hot plate TSS / VSS Water pollution process test method Vacuum filter, glass filter T-N UV measurement Resolver, HACH DR 4000 T-P Absorbance method Decomposition Device, Absorbance Agent

Table 1 shows a treatment plant operated by a catalytic oxidation method using a C-type contact medium 155a. Table 2 shows the case where the sewage treatment plant operated by the standard activated slab fj method was selected and the experimental apparatus was designed and operated according to the process of the present invention. The measurement and analysis methods are shown in Table 2-1.

The influent BOD load was operated in the range of 0.57-0.69 kg / m ³ days, and the influent sewage was treated by inflow into the tank at 13.8 L / hour. The hydraulic retention time was 2.1 hours for each anaerobic tank for anaerobic tank and 2.9 hours for aeration tank and nitriding tank for 10 hours.

Table 3. Removal Efficiency by Item

Item Inflow (mg / ℓ) Runoff (mg / ℓ) % Removal BOD 300 3 99 CODcr 420 35 92 CODmn 60 10 83 SS 140 5 96 T-N 36 7 80 T-P 3.8 One 73

The removal efficiency of BOD, CODcr, and SS was 99%, 92% and 96%, respectively. This is 5 to 10% increase compared to the processing efficiency of the existing method, it can be seen that the processing efficiency of 5% than the existing process of the first treatment example. In most biological treatment systems, the following three processes occur simultaneously. The process is quantitatively related to aerobic processes as follows.

A. Oxidation

COHNS + O2 + Bacteria → CO2 + NH3 + Other + Energy

(Organic) (final product)

B. Synthesis

COHNS + O2 + Bacteria + Energy → C5H7NO2

(Organic) (proliferating bacterial cells)

C. Endogenous Respiration (Autoxidation)

C5H7NO2 + 502 → 5CO2 + NH3 + 2H2O + Energy

In the above formula, COHNS represents organic matter in sewage, and C5H7NO2 represents a cell tissue. In the above formula, no enzyme plays a role, but in fact, the dissolution or degradation of the colloidal or particulate sludge is produced by bacteria. Proceeded by extra cellular enzymes. However, because of the specificity that many bacteria produce only when they are starved, the bacteria are abundant and do not produce enough extra-cellular enzymes during growth and division. Thus, the biggest cause of sludge reduction is the creation of conditions and conditions to produce large amounts of extra cellular enzymes.

Such a condition is sufficiently achieved by the carrier 155 filled in the rotary carrier charging device 15 according to the present invention. The specific surface area of the contact media is 400 m ² / m ³ , and after sludge is attached, the specific surface area is increased to 7,000-14,000 m ² / m ^{3, and} the attraction force of the suspended solids is strong. The adsorption and anaerobic aerobic treatment is carried out by a wide variety of microorganisms between the contact media. Biofilm in contact with the filter material is excellent in the adhesion of microorganisms and suspended solids and retention of the microorganism reaches to the average 300~900g per 1m ^2, tends to be concentrated to a high concentration and contribute to reduce the amount of sludge in the biological, physical. Also, microorganisms with slow growth rate can multiply without leaking to the outside, so the age of survival of sludge increases and the automatic oxidation of sludge is promoted. Excellent ability to cope with fluctuations, impact loads, and hard-decomposable material inflow, and eliminates problems such as swelling of sludge.

Although the above is an aerobic treatment method, the sludge is removed from the sedimentation layer by anaerobicization of the biofilm in the contact media and the replacement of new sludge is not easy. Rotating at a moderate speed rather than piles is beneficial for increasing final treatment efficiency.

The sludge reduction, one of the features of the present invention, was 5.8 g / year as the experimental result (50 days) TS. This was less than 1% compared with the activated sludge 0.20~0.25kg / m ³ relative to the flowing waste water 0.93g / m ^3. In other words, it shows remarkable characteristics compared with the existing sewage treatment method. The small amount of sludge is generated because the concentration of MLSS in the aeration tank and the nitriding tank is very small, about 5mg / L, and the sludge generated from the sludge is discharged as the clear nitriding solution flows into the settling tank. Therefore, it is an economical process to minimize the size of the sedimentation tank in the existing sewage treatment plant, and it is also an excellent countermeasure against unstable emergency during operation.

Although new microorganisms multiply as microorganisms decompose organic matter, the sludge is hardly discharged because the microorganisms produced are assetd. In this review of the sludge, which is based on organic matter, based on organic matter, BOD is 0.36 kg / m ³ .d, assuming that the yield of microorganisms (Y) at a general sewage treatment plant for 300 mg / L of influent BOD is 0.6. Based on this, the rate of assetization per unit area of contact media (damge) was 12.9g / m ³ .d, which was high.

Table 4. Total Surplus Sludge Generation

division Sludge Generation Avg g DS / Year Sludge amount per influent sewage (m ³ ) g DS / m ³ TS 5.8 0.93 VS 4.8 0.79

In the table above, the result of calculating the amount of sludge was found to be 5.8g of dry solids per year, but most of it was caused by the outflow of MLSS in the tank during abnormal operation. It is estimated that lower sludge will occur.

Nitrogen and phosphorus removal rate was another characteristic of the present invention was 80%, 73% respectively. This can be said to be a process that the nitrogen and phosphorus removal rate is significantly improved compared to the simultaneous nitrogen and phosphorus removal method mentioned above.

As the nitrogen concentration changes in each process, most of the nitrogen is removed from the anoxic tank and discharged. In the nitrogen removal structure, ammonia nitrogen is changed to nitrite nitrogen and nitrate nitrogen and then removed through denitrification. According to the present invention, the nitrate nitrogen oxidized in the aeration tank and the nitrification tank is denitrated in the anoxic process. The concentration of is mainly removed in the anaerobic process. In the case of phosphate phosphorus and total phosphorus, the removal structure is that phosphorus is released in anaerobic and absorption of phosphorus occurs in aerobic, which is a process of over-absorption and removal in aerobic process. In addition, phosphate phosphorus absorbed in aerobic conditions is removed when excess sludge is discharged. In this design, the efficiency of phosphorus removal is inferior to nitrogen removal efficiency because there is little sludge discharged without the need for a return sludge facility. However, it is relatively easy to remove phosphorus compared to nitrogen, so it is easy to install even if additional removal facilities are needed.

As described above, when the rotary filler filling device of the present invention removes nitrogen and phosphorus at the same time, it is not necessary to return sludge, thus saving the site and facility cost required, and unlike conventional methods, F / M ratio or SRT Since the factors can be omitted, the sludge swelling phenomenon does not occur, which is not necessary for professional management personnel, thus making maintenance easy and cost low.

In addition, the rotary filling device uses high efficiency contact media made of waste synthetic resin (HDPE), which is discarded after cultivation, as a tin to obtain the effect of two-million pairs of waste recycling and water treatment, and by rotating the filling device. Since it is possible to form a dense microbial membrane in the contact media, it is resistant to organic matter and load fluctuations of the influent and minimizes the generation of sludge by the settlement and high assetization of various microbial species.

Considering the fact that large-scale sewage treatment facilities are expected to strengthen the regulation of nitrogen and phosphorus discharge quality due to the tendency of many problems in construction and maintenance, and the transition to medium- and small-sized treatment methods for pollutant sources. The present invention is a sewage treatment device that meets the effluent water quality standards of nutrients, which is to reduce the construction cost of sewage treatment plant, ease of maintenance, stability of treatment efficiency, and strict regulation.

Claims (3)

A plurality of rotary shafts 151 are included in the phosphorus discharge tank 3, the anoxic tank 4, the first reaction tank 5, and the second reaction tank 6 of the sewage treatment facility installed to simultaneously remove nitrogen and phosphorus in the sewage. The plate 152 is installed side by side at a predetermined interval, and the compartment 154 formed by dividing the space between the porous plates 152 into radial spaces 153 is approximately divided into concentric circles and the sewage flowed into the outer circumference. Is attached to the screen (156,157) to guide the collection in the direction of the center when the rotation, and the rotary filling device is installed a carrier filling device (15) filled with the contact material 155 in each compartment (154). The rotary carrier filling apparatus according to claim 1, wherein the contact member (155) is a corrugated contact member (155b). The method of claim 2, wherein the corrugated contact material (155b) is mixed with a suitable amount of fine particles such as soil and stone powder in the waste synthetic resin (HDPE) and activated by carbonization by heating and melting to increase the adsorption capacity of the initial microorganism and induce the activation of various microorganism Rotary carrier filling device for sewage treatment for sewage treatment formed so that it can be.