CN113754058A - Wastewater treatment device and method based on two-stage A/O process - Google Patents
Wastewater treatment device and method based on two-stage A/O process Download PDFInfo
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/306—Pesticides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
Abstract
The invention relates to a wastewater treatment device based on a two-stage A/O process, which is characterized by comprising a first-stage A/O system, a second-stage A/O system and a secondary sedimentation tank. The water inlet pipelines of the first section of A/O system and the second section of A/O system are arranged in parallel and series connection at the same time, the nitrified liquid in the aeration tank flows back to the anoxic tank, and the sludge in the secondary sedimentation tank flows back to the anoxic tank. The present application also relates to a method for treating wastewater using a wastewater treatment plant as described above. The method solves the treatment problem of the high ammonia nitrogen organic wastewater, the high ammonia nitrogen wastewater can be directly subjected to biochemical treatment without pretreatment, the bottleneck that the denitrification efficiency of the traditional A/O process is limited by the reflux ratio is solved, the standard reaching of the total nitrogen of the effluent is ensured, and the method has the advantages of simple operation, low investment, high treatment efficiency of the ammonia nitrogen and the total nitrogen, wide application range and easy industrial application.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a wastewater treatment device based on two sections of anoxic tank (A)/aeration tank (O) processes and a method for treating high ammonia nitrogen organic wastewater by using the device.
Background
At present, the treatment of high ammonia nitrogen wastewater is a difficult problem in the sewage treatment industry. On one hand, the ammonia nitrogen concentration is too high to bring inhibition to biological treatment, and generally speaking, when the ammonia nitrogen concentration of a biochemical system reaches more than 50mg/L, the problems that nitration reaction is inhibited and the ammonia nitrogen concentration of effluent is increased are shown. Therefore, the wastewater with high ammonia nitrogen concentration is generally pretreated, and the pretreatment measures generally comprise a stripping method, an adsorption method, a precipitation method, an oxidation method and the like, but various pretreatment methods have the problems of high treatment cost, secondary pollution and the like, so that the direct biological treatment of the wastewater with high ammonia nitrogen concentration is the most economic, effective and promising method. The second aspect is that the biological treatment of high ammonia nitrogen wastewater has the problem that the total nitrogen of the effluent exceeds the standard, for example, the discharge standard of the fermentation pharmaceutical industry (GB21903-2008) requires that the ammonia nitrogen of the effluent is less than 35mg/L, the total nitrogen of the effluent is less than 70mg/L, and the total nitrogen concentration of the influent is close to 1000mg/L, so that the removal rate of the total nitrogen needs to be 95%, and the high removal rate is difficult to achieve by the existing sewage treatment process. Therefore, the effluent is usually further subjected to denitrification treatment, which results in high treatment cost.
For a long time, the total nitrogen index is not listed in the assessment range in the surface water environment quality assessment system, so that the attention degree of all places on the total nitrogen control is relatively insufficient, and the control strength is deficient. However, in recent years, nitrogen pollution has become a main factor of offshore area, lake and reservoir pollution, and has become a prominent bottleneck affecting the improvement of watershed water quality. It is expected that the national emission standard and supervision of total nitrogen will become more and more strict in the future, and especially the problem of reaching the standard of total nitrogen is more and more emphasized in the industries producing high ammonia nitrogen wastewater such as chemical industry, pharmacy, coking, nitrogenous fertilizer, livestock raising, slaughtering and the like and corresponding chemical industry parks.
For the treatment of high ammonia nitrogen wastewater, the A/O process is widely applied with the advantages of maturity and reliability. However, the removal of total nitrogen by the A/O process is limited in denitrification efficiency by the reflux ratio (R: the ratio of the reflux flow rate to the feed flow rate). Theoretically, the denitrification efficiency is R/(R +1), and the denitrification efficiency of the A/O process is 80-90%. In order to ensure the standard reaching, the current common practice is to carry out denitrification treatment after A/O. However, this requires consumption of carbon source, and the operation cost is high, and the organic matter remaining after denitrification causes a problem of increase in COD of the effluent. How to break through the limitation of reflux ratio of the A/O process and improve the denitrification rate of the A/O process becomes a big problem in the sewage treatment industry.
Therefore, there is a continuing need in the art to develop an apparatus and method for treating high ammonia nitrogen wastewater.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a wastewater treatment device based on a two-stage A/O process with high denitrification rate. Particularly, the high ammonia nitrogen wastewater is treated by adopting a two-stage A/O process, so that the technical problem in the field of sewage treatment is solved. In addition, certain measures are taken on the operation process and the operation equipment, the total nitrogen removal efficiency can be higher than that of theoretical calculation data, and the result shows that in the actual reaction process, the two sections of A/O processes are not only the combination of two A/O systems, but also various biochemical reactions of simultaneous nitrification and denitrification, partial nitrification and denitrification and anaerobic ammonia oxidation exist.
It is also an object of the present application to provide a method for treating wastewater by means of a wastewater treatment plant based on a two-stage a/O process as described above.
In order to achieve the object of the present invention, the present application provides the following technical solutions.
In a first aspect, the present application provides a wastewater treatment apparatus based on a two-stage a/O process, comprising a first stage a/O system, a second stage a/O system, and a secondary sedimentation tank;
the first stage A/O includes:
a first anoxic tank and a first aeration tank, which are connected in series with each other;
the first water inlet pipeline is used for inputting wastewater to be treated into the first anoxic pond;
a first water outlet line for outputting the wastewater treated by the first anoxic tank and the first aeration tank from the first aeration tank;
a first nitrified liquid return line for returning the nitrified liquid in the first aeration tank to the first anoxic tank;
the second segment A/O includes:
a second anoxic tank and a second aeration tank, which are connected in series with each other;
the second water inlet pipeline is used for inputting wastewater to be treated into the second anoxic pond;
a second water outlet line for outputting the wastewater treated by the second anoxic tank and the second aeration tank from the second aeration tank;
a second nitrified liquid return line for returning the nitrified liquid in the second aeration tank to the second anoxic tank;
wherein the secondary sedimentation tank is in fluid communication with the second outlet pipeline, and the secondary sedimentation tank returns sludge in the secondary sedimentation tank to the first anoxic tank and/or the second anoxic tank through a first sludge return pipeline;
wherein the first water inlet line and the second water inlet line are arranged in parallel;
wherein the first water outlet line is in fluid communication with the second anoxic tank.
In one embodiment of the first aspect, the first anoxic tank and the first aeration tank are configured as an integrated cycle;
the second anoxic tank and the second aeration tank are configured as an integrated cycle.
In one embodiment of the first aspect, the first anoxic tank and/or the second anoxic tank comprises an agitation device, preferably comprising one or more of an underwater propeller and a vertical agitator.
In one embodiment of the first aspect, the first aeration tank and the second aeration tank comprise aeration means, preferably comprising HS cut-through aerators manufactured by shanghai edge environmental engineering limited.
In one embodiment of the first aspect, the volume ratio of the first anoxic tank to the second anoxic tank is 1:1 to 2: 1.
In one embodiment of the first aspect, the first aeration tank and/or the second aeration tank is divided into 2 to 6 compartments, and the ratio of the length to the width of each compartment of the galleries is (4:1) to (10: 1).
In a second aspect, the present application provides a method of treating wastewater by a wastewater treatment plant based on a two-stage a/O process as described in the first aspect.
In one embodiment of the second aspect, the first anoxic tank, the second anoxic tank, the first aeration tank, or the second aeration tank comprises one or more of the following flora: bacteroides (Bacteroides), Proteobacteria (Proteobacteria), ammonia oxidizing bacteria (Nitrosomonas, Niosococcus, etc.), nitrite oxidizing bacteria (Nitrobacter, Nitrococcus, etc.), Pseudomonas (Pseudomonas), Achromobacter (Achromobacter), Alcaligenes (Alcaligenes), Anammox (Anammox).
In one embodiment of the second aspect, the effluent BOD of the first stage A/O system5The concentration of the ammonia nitrogen in the effluent is not more than 5 mg/L; BOD of effluent of the second section A/O system5Not more than 5mg/L, and the ammonia nitrogen of the effluent is not more than 5 mg/L.
In one embodiment of the second aspect, the average sludge concentration of the first stage A/O system and the second stage A/O system is between 6g/L and 15 g/L.
In one embodiment of the second aspect, the COD load of the first stage a/O system and the second stage a/O system is 0.05 to 0.1 gpod/(gMLVSS-d).
In one embodiment of the second aspect, theThe denitrification degradation rate of the first anoxic tank and/or the second anoxic tank is 0.05-0.2 gNO3-N/(gMLVSS·d)。
In one embodiment of the second aspect, the wastewater to be treated has COD and NO3The ratio-N is 4-5.
In one embodiment of the second aspect, the dissolved oxygen DO of the first anoxic tank and/or the second anoxic tank is less than 0.5mg/L, and the pH is 6.5 to 7.5.
In one embodiment of the second aspect, the nitrification reaction rate of the first aeration tank and/or the second aeration tank is 3 to 6mgNH3-N/(L·h)。
In one embodiment of the second aspect, the dissolved oxygen DO at the end of the first aeration tank and/or the end of the second aeration tank is 3-6 mg/L.
In one embodiment of the second aspect, the reflux ratio of the nitrifying liquid of the first-stage A/O system is 4-10; and the reflux ratio of the nitrifying liquid of the second section of A/O system is 4-10.
In one embodiment of the second aspect, the surface load of the secondary sedimentation tank is 0.5 to 0.75m3/(m2·h)。
In one embodiment of the second aspect, the sludge reflux ratio of the secondary sedimentation tank is 1-2.
In one embodiment of the second aspect, the ammonia nitrogen concentration of the wastewater to be treated is less than or equal to 2000 mg/L.
Compared with the prior art, the invention has the beneficial effects that: (1) the problem of toxicity of high ammonia nitrogen to the wastewater is solved, and the biochemical treatment is directly carried out without pretreatment; (2) the bottleneck that the denitrification efficiency of the existing A/O process is limited by the reflux ratio is overcome, the actual denitrification efficiency reaches over 95 percent and exceeds the theoretical denitrification efficiency; (3) the investment is saved, the operation is simple and convenient, the operation cost is low, and the maintenance is easy; (4) wide application range, easy popularization and application, and is suitable for treating high ammonia nitrogen industrial wastewater and urban sewage and industrial park sewage with high requirement on total nitrogen treatment.
Drawings
FIG. 1 is a schematic view of a wastewater treatment apparatus based on a two-stage A/O process according to example 1.
FIG. 2 is a schematic view of a wastewater treatment apparatus based on a two-stage A/O process according to example 2.
In the above figures, the reference numerals have the following meanings:
11 first anoxic tank
12 first aeration tank
13 second anoxic tank
14 second aeration tank
15 secondary sedimentation tank
101 first water inlet pipeline
102 second water inlet pipeline
103 first nitrified liquid reflux pipeline
104 second nitrified liquid return line
105 first sludge return line
106 first water outlet line
107 second water outlet line
108 secondary sedimentation tank water outlet pipeline
200 water inlet main pipeline
21 first series of first anoxic tanks
22 first series of first aeration tanks
23 second anoxic tank of the first series
24 second aeration tank of the first series
25 first series of secondary sedimentation tanks
26 three-sedimentation tank
201 first series of first water inlet lines
202 first series of second water inlet lines
203 first series of first nitrated liquid return lines
204 first series of second nitrated liquid return lines
205 first series of first sludge recirculation lines
206 first series of first outlet lines
207 second water outlet line of the first series
208 first series of secondary sedimentation tank water outlet pipelines
209 three-sedimentation tank water outlet pipeline
31 first anoxic tank of second series
32 first aeration tank of second series
33 second series of second anoxic tanks
34 second series of second aeration tanks
35 second series of secondary sedimentation tanks
301 first water inlet line of the second series
302 second series of second water inlet lines
303 first nitrating liquid reflux line of second series
304 second series of second nitrated liquid return lines
305 first sludge return line of the second series
306 first water outlet line of the second series
307 second series of second water outlet lines
308 second series of secondary settling tanks.
Detailed Description
Unless otherwise defined, technical or scientific terms used herein in the specification and claims should have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. All numerical values recited herein as between the lowest value and the highest value are intended to mean all values between the lowest value and the highest value in increments of one unit when there is more than two units difference between the lowest value and the highest value. In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings, which are merely for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be construed as limiting the invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the invention, the meaning of "a plurality" is two or more unless otherwise specified.
In the description of the invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "connected" and "connected" are to be construed broadly, e.g. as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the creation of the present invention can be understood by those of ordinary skill in the art through specific situations.
In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, where it is noted that in the interest of brevity and conciseness, not all features of an actual embodiment may be described in detail in this specification. Modifications and substitutions to the embodiments of the present invention may be made by those skilled in the art without departing from the spirit and scope of the present invention, and the resulting embodiments are within the scope of the present invention.
As mentioned above, the existing A/O process has insufficient nitrogen removal efficiency when treating high ammonia-nitrogen wastewater due to the limitation of reflux ratio. After the A/O process treatment, the denitrification treatment is carried out separately, which not only causes the increase of the cost, but also causes the increase of the COD effluent of the final effluent.
In order to solve the technical problem, the application provides a wastewater treatment device based on two-stage A/O technology, so that high ammonia nitrogen organic wastewater respectively enters two stages of A/O systems under the condition of no pretreatment, and effluent of a first stage A/O system enters a second stage A/O system. The first stage and second stage a/O systems of the wastewater treatment plants described herein are in both series and parallel relationship. And a nitrified liquid return line is arranged in each section of the A/O system. In addition, the wastewater treatment device also comprises a secondary sedimentation tank, wherein the secondary sedimentation tank returns sludge to the anoxic tank through a sludge return line, so that nitrification, denitrification, short-cut nitrification and denitrification, simultaneous nitrification and denitrification and anaerobic ammonia oxidation reactions can be simultaneously carried out in the anoxic tank and/or the aeration tank, and the synergistic effect of various floras is obvious.
In one embodiment, the application provides a device for removing high ammonia nitrogen organic wastewater by a two-stage A/O process, which is characterized in that the high ammonia nitrogen wastewater enters a first-stage A/O system and a second-stage A/O system respectively, and the two-stage A/O systems are connected in parallel from the water inlet. And simultaneously, the effluent of the first section of A/O system enters a second section of A/O system, and the two sections of A/O systems are connected in series. Thus fully utilizing the organic carbon source of the inlet water and reducing the cost of additionally supplementing the carbon source. In addition, the two sections of A/O have nitration liquid reflux, which is equal to the improvement of the reflux ratio of the nitration liquid. And finally, the effluent of the first section has a diluting effect on the influent of the second section, so that the concentration of toxic substances is reduced, and the denitrification rate is higher. The total nitrogen comprises organic nitrogen, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen. The traditional A/O process is a pre-denitrification process, wastewater sequentially passes through an anoxic tank, an aerobic tank and a secondary sedimentation tank, nitrification liquid flows back from the aerobic tank to the anoxic tank, and sludge flows back from the secondary sedimentation tank to the anoxic tank.
In one embodiment, the high ammonia nitrogen wastewater can directly enter an A/O system for treatment without pretreatment measures such as stripping, and the concentration of the ammonia nitrogen in the inlet water can reach 2000mg/L, such as 900mg/L, 1000mg/L, 1500mg/L or 2000 mg/L.
In one embodiment, the anoxic tank and the aeration tank are in an integrated circulation mode, the same reaction tank contains multiple floras, nitrification, denitrification, short-cut nitrification and denitrification, simultaneous nitrification and denitrification and anaerobic ammonia oxidation reactions exist simultaneously, and the synergistic effect of the various floras is obvious.
In one embodiment, biological nitrification is a prerequisite for biological denitrification, and only good nitrification is achievedHigh efficiency and stable denitrification. Thus, each A/O system is biodegraded to the limit, the effluent BOD of each A/O5Not more than 5mg/L, and the ammonia nitrogen of the effluent is not more than 5 mg/L.
In one embodiment, the average sludge concentration of the two-stage A/O system is between 6g/L and 15 g/L. For example, the average sludge concentration of the two-stage A/O system can be 6g/L, 7g/L, 8g/L, 9g/L, 10g/L, 11g/L, 12g/L, 13g/L, 14g/L, 15g/L, or a range or subrange between any two of them.
In one embodiment, the COD load of the two-stage A/O system is 0.05-0.1 gCOD/(gMLVSS.d).
In one embodiment, the anoxic tank performs agitation treatment while treating the wastewater. In a preferred embodiment, adequate mixing of the sludge and wastewater can be ensured by installing an underwater propeller or a vertical mixer. In a preferred embodiment, the underwater propeller has a power of l to 2W/m3Selecting the type, wherein the vertical stirring power is 5-15W/m3And (4) selecting the type, wherein specific data are selected according to the type of the reaction tank and the performance of equipment.
In one embodiment, the denitrification degradation rate of the anoxic tank is 0.05-0.2 gNO3-N/(gMLVSS · d). In a preferred embodiment, the denitrification degradation rate in the first anoxic tank and/or the second anoxic tank is 0.05-0.10 gNO3N/(gMLVSS. d), preferably at 20-30 ℃, DO less than 0.5mg/L, pH 6.5-7.5, C: n ═ 4-5: 1.
in one embodiment, to ensure good total nitrogen removal, it is desirable to ensure that the influent COD and NO are both present3the-N ratio is 4-5, otherwise, additional carbon source supplement is required.
In one embodiment, the nitrification reaction rate of the aeration tank is 3-6 mgNH3-N/(L.h), preferably at a temperature of 20-30 ℃.
In one embodiment, the dissolved oxygen DO at the tail end of each aeration tank is controlled to be 3-6 mg/L, the pH value is 7.0-8.0, and the reflux ratio of the nitrifying liquid of each section of A/O is 4-10.
In one embodiment, the aeration tank employs a conventional aerobic activated sludge processThe aeration device is preferably an HS forced-cutting aerator produced by Shanghai edge environmental engineering Limited, and the ventilation rate of each aerator is 1.0-2.0 m3And/min, the aerators are linearly arranged, and the air flow rate of the main air pipe is 8-12 m/s.
In one embodiment, the aeration tank can be divided into 2 to 6 compartments, and the ratio of the length to the width of each compartment of the gallery is (4:1) to (10: 1). The width of the corridor is generally 7.5-10.0 meters, and the depth of the pool is generally 5.0-7.0 meters.
In one embodiment, the total volume of the A/O system is determined according to the total COD (chemical oxygen demand) and the total ammonia nitrogen content of the wastewater, and the COD load is generally 0.05-0.1 gCOD/(gMLVSS.d); the volume of the anoxic pond is determined according to the denitrification rate, and 0.05-0.2 gNO is generally taken3-N/(gMLVSS · d). In one embodiment, the volume ratio of the first anoxic tank to the second anoxic tank is 1:1 to 2: 1. When the concentration of toxic substances in the wastewater is higher, the value is smaller, and when the concentration of ammonia nitrogen in the wastewater is higher, the value is larger.
In one embodiment, the wastewater after two-stage A/O treatment enters a secondary sedimentation tank, and the surface load of the secondary sedimentation tank is preferably 0.5-0.75 m3/(m2H), the water depth of the secondary sedimentation tank is preferably 5-6.5 m, supernatant is discharged after sedimentation, and the sedimented sludge flows back to the first anoxic tank, wherein the preferable sludge backflow ratio is 1-2.
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention.
In the following examples, COD and NH3N, TN and SS were measured according to the methods for Water and wastewater monitoring and analysis, environmental science publishers, fourth edition, 2002, China; the method specifically comprises the following steps: the COD detection method is a GB11914-89 potassium Choeroate method; NH (NH)3the-N detection method is GB7478-87 Nashin reagent photometry; the TN detection method is GB11894-89 potassium persulfate oxidation ultraviolet spectrophotometry; the SS detection method is GB11901-89 weight method.
Example 1
Urban sewage treatment device based on two-stage A/O process disclosed by the invention is utilized to treat urban sewageAnd (5) upgrading and transforming the plant. The urban sewage treatment plant is designed to treat 7500m of domestic wastewater3D, 7500m of industrial park sewage3And d, the COD of the inlet water is 500mg/L, the total nitrogen of the inlet water is 100mg/L, the sewage plant originally adopts a CWSBR process, the COD of the outlet water is 50mg/L, the ammonia nitrogen of the outlet water is 5mg/L, and the total nitrogen of the outlet water is 20 mg/L.
And (3) transforming and upgrading the sewage plant, and adding two sections of A/O systems and a secondary sedimentation tank, which are specifically shown in figure 1. The newly added sewage treatment device comprises a first section of A/O system and a second section of A/O system. The first stage a/O system includes a first anoxic tank 11 and a first aeration tank 12 connected in series with each other. The second stage a/O system includes a second anoxic tank 13 and a second aeration tank 14 connected in series with each other. The outlet line 107 of the second aeration tank 14 is in fluid communication with the secondary sedimentation tank 15. In the first stage a/O system, the nitrified liquid in the first aeration tank 12 is returned to the first anoxic tank 11 through the first nitrified liquid return line 103. In the second stage a/O system, the nitrified liquid in the second aeration tank 14 is returned to the second anoxic tank 13 through the second nitrified liquid return line 104. Further, the sludge in the secondary sedimentation tank 15 is returned to the first anoxic tank 11 through the first sludge return line 105. It is to be noted that the sludge in the secondary sedimentation tank 15 may also be returned to the second anoxic tank 13 through the first sludge return line 105.
The high ammonia nitrogen organic wastewater can enter the first anoxic tank 11 through the first water inlet pipeline 101 and enter the second anoxic tank 13 through the second water inlet pipeline 102. The first water inlet line 101 and the second water inlet line 102 are parallel lines. In addition, the water outlet line 106 of the first aeration tank 112 is in fluid communication with the second anoxic tank 13. The arrangement is such that the first stage A/O system and the second stage A/O system are in a series and parallel relationship simultaneously.
First anoxic pond volume 3700m3The volume of the first aeration tank is 7700m3Second anoxic pond volume 3700m3The volume of the second aeration tank is 7700m3Surface load of secondary sedimentation tank is 0.75m3/(m2H), installing 4 underwater propellers in the first anoxic pond and the second anoxic pond, wherein the power of the propellers is 2.5kW, installing 3 magnetic suspension fans, the power of the fans is 200kW, and installing 287 sets of HS forced-cutting aerators. The reflux ratio of the nitrifying liquid from the first aeration tank to the first anoxic tank is4:1, the reflux ratio of nitrifying liquid from the second aeration tank to the second anoxic tank is 4:1, and the reflux ratio of sludge is 1.5: 1. COD of outlet water from 107 after reconstruction<30mg/L, ammonia nitrogen in effluent<1mg/L, total nitrogen of effluent<8 mg/L. The treated wastewater can be discharged through the outlet line 108 of the secondary sedimentation tank 15.
Example 2
The product of the waste water produced in a large pharmaceutical factory comprises veterinary drugs (tilmicosin, tilmicosin phosphate, flunixin meglumine and the like), semisynthetic antibiotics, cephalosporins, tylosin, salinomycin, spectinomycin, acetylspiramycin, abamectin, 7ACA and the like. Designed water volume 10500m3And d, influent COD4500mg/L and total influent nitrogen 400 mg/L.
The sewage treatment apparatus of this embodiment is constructed as shown in FIG. 2. The biochemical treatment of this example employs a two-stage a/O treatment system comprising two identical two-stage a/O series, the direct connection of the first anoxic tank, the first aeration tank, the second anoxic tank, and the second aeration tank of each series being the same as that shown in example 1. The difference is that the waste water is input into each series after being input through the water inlet main pipeline 200, and the water outlet pipeline of each series of secondary sedimentation tanks is communicated with the fluid of the tertiary sedimentation tank 26.
Taking one of the series as an example, the first anoxic tank volume is 4500m3Volume of the first aeration tank is 16500m3The volume of the second anoxic pond is 4500m3Volume of the second aeration tank is 16500m3Surface load of secondary sedimentation tank is 0.5m3/(m2H), installing 4 underwater propellers in the first anoxic pond and the second anoxic pond, wherein the power of the propellers is 3.1kW, installing 6 magnetic suspension fans, the power of the fans is 200kW, and installing a set of HS forced-cutting aerators 540. The nitrifying liquid reflux ratio of O1 to A1 is 8:1, the nitrifying liquid reflux ratio of O2 to A2 is 8:1, and the sludge reflux ratio is 2: 1. The MLSS in the system is 10g/L, and the DO at the tail end of each aeration tank (24,34) is 4-6 mg/L. COD of effluent<300mg/L, ammonia nitrogen in effluent<3mg/L, total nitrogen of effluent<15 mg/L. The treated wastewater can be discharged through the outlet line 209 of the tertiary sedimentation tank 26.
Example 3
The sewage treatment plant is concentrated in a certain pharmaceutical park, and the pharmaceutical types comprise aureomycin and hydrochloric acidChlortetracycline, terramycin, penicillin, coenzyme Q10, pesticide, veterinary drug, enzyme preparation, etc. Design water quantity 12000m3D, inflow COD10000mg/L, and inflow total nitrogen 800 mg/L.
The sewage treatment apparatus of this example comprises four two-stage A/O trains. Taking one of the series as an example, the first anoxic tank volume 6100m3First aeration tank volume 17000m3The volume of the second anoxic tank is 6100m3Second aeration tank volume 17000m3Surface load of secondary sedimentation tank is 0.5m3/(m2H), installing 4 underwater propellers in the first anoxic pond and the second anoxic pond, wherein the power of the propellers is 3.1kW, installing 6 magnetic suspension fans, the power of the fans is 200kW, and installing a set of HS forced-cutting type aerators 560. The nitrifying liquid reflux ratio of O1 to A1 is 10:1, the nitrifying liquid reflux ratio of O2 to A2 is 10:1, and the sludge reflux ratio is 2: 1. The MLSS in the system is 12-15 g/L, and the DO at the tail end of each aeration tank is 4-6 mg/L. COD of effluent<60mg/L, ammonia nitrogen in effluent<5mg/L, total nitrogen of effluent<15mg/L。
The embodiments described above are intended to facilitate the understanding and appreciation of the application by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present application is not limited to the embodiments herein, and those skilled in the art who have the benefit of this disclosure will appreciate that many modifications and variations are possible within the scope of the present application without departing from the scope and spirit of the present application.
Claims (19)
1. A wastewater treatment device based on two-stage A/O process is characterized by comprising a first-stage A/O system, a second-stage A/O system and a secondary sedimentation tank;
the first stage A/O includes:
a first anoxic tank and a first aeration tank, which are connected in series with each other;
the first water inlet pipeline is used for inputting wastewater to be treated into the first anoxic pond;
a first water outlet line for outputting the wastewater treated by the first anoxic tank and the first aeration tank from the first aeration tank;
a first nitrified liquid return line for returning the nitrified liquid in the first aeration tank to the first anoxic tank;
the second segment A/O includes:
a second anoxic tank and a second aeration tank, which are connected in series with each other;
the second water inlet pipeline is used for inputting wastewater to be treated into the second anoxic pond;
a second water outlet line for outputting the wastewater treated by the second anoxic tank and the second aeration tank from the second aeration tank;
a second nitrified liquid return line for returning the nitrified liquid in the second aeration tank to the second anoxic tank;
wherein the secondary sedimentation tank is in fluid communication with the second outlet line, and sludge in the secondary sedimentation tank is returned to the first anoxic tank and/or the second anoxic tank through a first sludge return line;
wherein the first water inlet line and the second water inlet line are arranged in parallel;
wherein the first water outlet line is in fluid communication with the second anoxic tank.
2. The wastewater treatment plant according to claim 1, wherein the first anoxic tank and the first aeration tank are configured as an integrated cycle;
the second anoxic tank and the second aeration tank are configured as an integrated cycle.
3. The wastewater treatment plant according to claim 1 or 2 based on a two stage a/O process, wherein the first anoxic tank and/or the second anoxic tank comprises a stirring device, preferably comprising one or more of an underwater propeller and a vertical stirrer;
the first aeration tank and the second aeration tank include an aeration device, which preferably includes an HS cut-through aerator manufactured by shanghai edge environmental engineering limited.
4. The wastewater treatment apparatus based on the two-stage A/O process according to claim 1 or 2, wherein the volume ratio of the first anoxic tank to the second anoxic tank is 1:1 to 2: 1.
5. The wastewater treatment apparatus according to claim 1 or 2, wherein the first aeration tank and the second aeration tank are divided into 2 to 6 compartments, and the ratio of the length to the width of each compartment of the galleries is (4:1) to (10: 1).
6. A method for treating wastewater by the wastewater treatment plant based on the two-stage a/O process according to claim 1.
7. The method of claim 6, wherein the first anoxic tank, the second anoxic tank, the first aeration tank, or the second aeration tank comprises one or more of the following flora:
bacteroides (Bacteroides), Proteobacteria (Proteobacteria), ammonia oxidizing bacteria (Nitrosomonas, Niosococcus, etc.), nitrite oxidizing bacteria (Nitrobacter, Nitrococcus, etc.), Pseudomonas (Pseudomonas), Achromobacter (Achromobacter), Alcaligenes (Alcaligenes), and Anammox (Anammox).
8. The method of claim 6, wherein the effluent BOD of the first stage a/O system5The concentration of the ammonia nitrogen in the effluent is not more than 5 mg/L; BOD of effluent of the second section A/O system5Not more than 5mg/L, and the ammonia nitrogen of the effluent is not more than 5 mg/L.
9. The method of claim 6, wherein the average sludge concentration of the first stage a/O system and the second stage a/O system is between 6g/L and 15 g/L.
10. The method of claim 6, wherein the COD load of the first stage a/O system and the second stage a/O system is 0.05 to 0.1 gpod/(gmlvvss-d).
11. The method of claim 6, wherein the first anoxic tank and/or the second anoxic tank have a denitrification degradation rate of 0.05 to 0.2gNO3-N/(gMLVSS·d)。
12. The method according to claim 6, wherein the wastewater to be treated has COD and NO3The ratio-N is 4-5.
13. The method of claim 6, wherein the first anoxic tank and the second anoxic tank have a dissolved oxygen DO of less than 0.5mg/L and a pH of 6.5 to 7.5.
14. The method of claim 6, wherein the nitrification reaction rate of the first aeration tank and the second aeration tank is 3 to 6mgNH3-N/(L·h)。
15. The method according to claim 6, wherein the dissolved oxygen DO at the end of the first aeration tank and the end of the second aeration tank is 3 to 6 mg/L.
16. The method of claim 6, wherein the nitrifying liquid reflux ratio of the first stage A/O system is 4 to 10; and the reflux ratio of the nitrifying liquid of the second section of A/O system is 4-10.
17. The method according to claim 6, wherein the surface load of the secondary sedimentation tank is 0.5 to 0.75m3/(m2·h)。
18. The method according to claim 6, wherein the sludge reflux ratio of the secondary sedimentation tank is 1-2.
19. The method according to any one of claims 6 to 18, wherein the ammonia nitrogen concentration of the wastewater to be treated is less than or equal to 2000 mg/L.
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