CN108706730B - Biological nitrogen and phosphorus removal method with low carbon-nitrogen ratio - Google Patents
Biological nitrogen and phosphorus removal method with low carbon-nitrogen ratio Download PDFInfo
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- 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
- C02F3/302—Nitrification and denitrification treatment
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- 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
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- 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
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a biological nitrogen and phosphorus removal method with a low carbon-nitrogen ratio, and belongs to the field of sewage treatment. The sewage of the invention passes through the reaction tank and the secondary sedimentation tank in sequence to realize enhanced nitrogen and phosphorus removal, the TP removal rate is more than 90 percent or the effluent TP is less than 1mg/L, the delta BOD/delta TN is less than 4, the maximum flow flux of each area in the system is not more than 2.2Q, the sludge phosphorus content of the return sludge is more than 4 percent, and the invention has the advantages of high-efficiency nitrogen and phosphorus removal, energy-saving and low carbon operation, high load, land occupation saving, realization of the denitrification and phosphorus removal, no limit of the TN removal rate by the reflux ratio, simple control, convenient operation and management and the like. The system of the invention consists of a reaction tank, a secondary sedimentation tank and a connecting pipeline, wherein the reaction tank sequentially comprises a pre-anoxic zone, an anaerobic zone, a secondary sedimentation zone, an aerobic nitrification zone, a denitrification zone, an aerobic decarbonization zone and a water outlet zone from a water inlet end to a water outlet end, the connecting pipeline comprises a main water inlet pipe, a branch water inlet pipe, a water outlet pipe, a sludge overrunning pipe, a sludge return pipe, a residual sludge discharge pipe and the like, and the process flow is simple.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a low carbon-nitrogen ratio biological nitrogen and phosphorus removal method.
Background
The biochemical treatment of sewage is based on the traditional nitrogen and phosphorus removal mechanism. Denitrification process, including nitrification and denitrification; nitration, i.e. autotrophic nitrifying bacteria (AOB, NOB) under aerobic conditions, NH 4 + -N→NO 2 - -N→NO 2 - -N; denitrification, i.e. the denitrifying bacteria flora in anoxic conditions with NO X - Is an electron acceptor, an organic substance is an electron donor, NO 3 - -N→NO 2 - -N→N 2 . Biological phosphorus removal process, including anaerobic phosphorus release, aerobic transition phosphorus absorption, and discharge of excess sludge to realize biological phosphorus removal; in the anaerobic process, the phosphorus accumulating bacteria absorb organic matters and store the organic matters in cells to release phosphate; during aerobic, the organic matters stored in the cells are oxidized by dissolved oxygen to absorb the phosphorus in the water body. As can be seen, the core of denitrification and dephosphorization comprises three groups of flora, namely nitrifying flora, denitrifying flora and phosphorus-accumulating flora. The nitrifying bacteria belong to autotrophic bacteria, are strictly aerobic and have a lower specific growth rate; most of the denitrifying flora belongs to the heterotrophic bacteria, and the specific growth rate is high; the specific growth rate of the facultative anaerobe of the genus polyphosphate is high. In the typical treatment process of the current sewage plant, activated sludge is mostly adoptedAccording to A 2 the/O process is arranged in three stages, namely an anaerobic stage, an anoxic stage and an aerobic stage, nitrifying liquid flows back to the anoxic stage from the aerobic end to provide nitrate for denitrification, and other processes are mostly based on A 2 Deformation process of/O.
Typical of A 2 the/O process suffers from the following inherent disadvantages:
1) the nitrogen and phosphorus removal has a contradiction on sludge age, denitrifying flora and phosphorus accumulating flora need short sludge age, nitrifying flora needs long sludge age, but only single sludge age exists in the system, and the nitrogen and phosphorus removal is realized by adopting an intermediate method; but for nitrifying bacteria, the sludge age is insufficient, the treatment effect in winter is not ideal, and the treatment effect is unstable when the inlet water fluctuates; for denitrifying flora and phosphorus accumulating flora, the sludge age is too long, the sludge has an aging trend, and the treatment efficiency is reduced;
2) the nitrogen and phosphorus removal has the difference of dissolved oxygen demand, the phosphorus-accumulating bacteria need absolute anaerobism for anaerobic phosphorus release, the anaerobic phosphorus release process can be influenced or even inhibited by the existence of the dissolved oxygen, and the aerobic stage can excessively absorb phosphorus only when the anaerobic phosphorus release is more sufficient, so that good biological phosphorus removal is realized; the nature of the denitrification process is that the denitrifying bacteria react with NO x - The organic matter is an electron acceptor, and if molecular dissolved oxygen exists, the molecular dissolved oxygen can be preferentially used as the electron acceptor, so that the denitrification efficiency is influenced; the nitrifying flora is strictly aerobic, and anaerobism and carbon source can be inhibited, so that the HRT of the aerobic section in the traditional process is greater than the comprehensive HRT of other process sections, so as to ensure the basic metabolism of the nitrifying flora; for the activated sludge method, the activated sludge is a mixing system, each function is realized by separating each process section, but the functions are still restricted with each other, and the method comprises the spatial arrangement of each process section, the design of HRT and the like;
3) the nitrogen and phosphorus removal exists in competition on carbon sources, phosphorus-accumulating bacteria can only utilize volatile fatty acid in organic matters, and organic matters in other forms can be utilized by the phosphorus-accumulating bacteria only by hydrolyzing the organic matters into the volatile fatty acid; the requirement of the denitrifying flora on a carbon source is slightly lower than that of the phosphorus-accumulating bacteria, but only low-carbon organic matters can be utilized, and the competition of the quality and the quantity of the carbon source exists between the denitrifying flora and the phosphorus-accumulating bacteria; the biological denitrification generally requires that the C/N of inlet water is more than 4, the C/N of inlet water is more than 7 when in biological denitrification and dephosphorization, and the C/N of inlet water of domestic general domestic sewage is generally less than 4, which belongs to the shortage of carbon source and needs to be added with carbon source; the nitrifying bacteria are autotrophic, organic carbon sources are not needed, and the organic carbon sources can inhibit the metabolism of the nitrifying bacteria when exceeding a certain amount.
The nature of the denitrification process is NO X - Is an electron acceptor, and organic matters are electron donors; the nature of the aerobic phosphorus absorption of the phosphorus accumulating bacteria is that oxygen is taken as an electron acceptor, and organic matters are taken as an electron donor; if the phosphorus accumulating bacteria can produce NO X - The organic matter is an electron donor, so that 'one carbon dual-purpose' denitrification dephosphorization can be realized, the requirement of inlet water on C/N is reduced, and the carbon source consumption of sewage treatment is reduced; the research of molecular biology finds that the denitrification dephosphorization phenomenon lays a foundation for denitrification dephosphorization in the path, and the generation of the denitrification dephosphorization process can be promoted by creating environments of high-concentration phosphate, nitrate and organic matters.
In addition, sludge-aged flora such as nitrifying flora and the like is separated from short sludge-aged flora such as denitrifying flora and phosphorus accumulating bacteria, so that sludge-aged separation is realized. The strain separation method comprises a double-mud system, addition of a biological membrane and the like. The double-sludge system, namely two sets of biological systems, respectively bear the long-sludge-age and short-sludge-age flora, and has the disadvantages of complex system structure, high control difficulty, high requirement on operation management and difficulty in large-area application in engineering. In the conventional A 2 In the/O, a biological film is added, if a fixed filler is arranged in an aerobic zone, but the hydraulic shear provided by normal aeration is not enough to promote the normal update of microorganisms on the fixed filler, a dead sludge zone is generated in long-term operation, and the nitrification efficiency is seriously reduced; if in conventional A 2 Although a sludge-membrane composite process is formed by loading the suspension carrier in the/O, conditions cannot be created for denitrifying phosphorus removal, and when the concentration of the suspended sludge in the system is too high, the suspended sludge and a biological membrane on the suspension carrier compete to reduce the nitrification efficiency.
Disclosure of Invention
Based on the technical problems, the invention provides a biological nitrogen and phosphorus removal method with a low carbon-nitrogen ratio.
The technical solution adopted by the invention is as follows:
a biological nitrogen and phosphorus removal method with low carbon-nitrogen ratio is characterized in that inlet water sequentially passes through a reaction tank (S0) and a secondary sedimentation tank (S2) to remove pollutants; the reaction tank (S0) is sequentially provided with a pre-anoxic zone (PreA), an anaerobic zone (AP), a middle sedimentation zone (S1), an aerobic nitrification zone (ON), a denitrification zone (ANP), an aerobic decarburization zone (OC) and a water outlet zone (CS) from a water inlet end to a water outlet end.
Preferably, the residence time of the pre-anoxic zone (PreA) is 0.5-1.0h, the residence time of the anaerobic zone (AP) is 1.5-2.5h, the residence time of the intermediate settling zone (S1) is 1.5-3.0h, the residence time of the aerobic decarbonization zone (OC) is 0.5-2.0h, and the residence time of the effluent zone (CS) is less than or equal to 0.5 h.
Preferably, the aerobic nitrification zone (ON) has a nitrification area load of 0.0005-0.0015kgN/m 2 The organic area load of the aerobic decarbonization area (OC) is 0.004-0.012kgBOD/m 2 And d, the denitrification sludge load of the denitrification Area (ANP) is 0.03-0.06 kgN/kgMLSS/d.
Preferably, the sludge concentration of the aerobic nitrification area (ON) is less than 0.5g/L, and the sludge concentration of the anaerobic Area (AP), the denitrification Area (ANP), the aerobic decarburization area (OC) and the water outlet area (CS) is 3-8 g/L; the sludge age of the suspended sludge in the system is 4-12 days.
Preferably, the inflow flow rate is Q, the flow rate of the main water inlet pipe (P1) is 80% -90% Q, the flow rate of the sludge return pipe (P5) is 30% -120% Q, and the flow rate of the sludge surpassing pipe (P4) is 85% -100% of that of the sludge return pipe (P5).
Preferably, the DO of the aerobic nitrification zone (ON) is 2.0-6.0mg/L, the DO of the aerobic decarbonization zone (OC) is 1.5-4.5mg/L, and the DO of the effluent zone (CS) is 1.0-3.0 mg/L.
Preferably, when the ammonia nitrogen at the water outlet end of the aerobic nitrification area (ON) is less than 1.5mg/L, the DO is reduced, the reduction is not more than 15% every time, and the adjustment interval is at least 4h every time; when the ammonia nitrogen at the water outlet end of the aerobic nitrification area (ON) is more than 3mg/L, the DO is increased, the increase is not more than 15% every time, and the adjustment interval is at least 4h every time.
Preferably, the TP removal rate is more than 90 percent or the effluent TP is less than 1mg/L and delta BOD/delta TN is less than 4; the maximum flux of each area in the system does not exceed 2.2Q; the sludge phosphorus content of the return sludge is more than 4 percent.
As is well known to those skilled in the art, the effluent zone (CS) is mainly used to stabilize the liquid level and to reduce the effluent DO, and stirring or a small amount of aeration may be provided to prevent sludge settling; the aeration can be carried out by adopting micropore aeration or perforated pipe aeration; the perforated plate has the advantages that the size of the opening is smaller than the diameter of the suspension carrier, the filler loss is prevented, the area of the perforated plate is calculated according to the flow flux and the flow velocity of the via hole, and the flow velocity of the via hole is generally not more than 60 m/h.
As is well known to those skilled in the art, the flow rate of the sludge return pipe (P5) is RQ, R is the sludge reflux ratio, R is generally between 30% and 120%, R is generally selected according to the sludge characteristics to ensure a typical sludge concentration in the reactor of between 60% and 100%.
As is well known to those skilled in the art, the selection of sludge concentration is influenced by the quality of the influent water, and reasonable sludge concentration is selected on the premise of sludge age control.
As is well known to those skilled in the art, the residence time and the tank volume design of the denitrification zone are determined based on the denitrification rate; the residence time value of each partition can be determined according to design experience and industry specifications within the specified range of the invention.
As well known by people in the industry, the filling rate, namely the natural accumulation volume of the added suspension carriers and the proportion of the tank volume of an adding area, is less than or equal to 60 percent in order to ensure that the fillers can not accumulate in the tank under the normal aeration condition;
the void ratio is the percentage of the void volume of the suspension carrier in unit volume to the total volume, the larger the void ratio is, the smaller the influence of adding the suspension carrier on the tank volume is, for example, when the void ratio is 90%, 1m 3 The volume of the suspension carrier is 0.1m when the tank capacity is 100 percent 3 At a filling rate of 50%, the volume of the suspension carrier itself is 0.05m 3 ；
Specific surface area, i.e. the ratio of the surface area provided per unit of suspended carrier to the unit volume of the suspended carrier naturally accumulated, in m 2 /m 3 ；
Delta BOD/Delta TN, i.e. (BOD of system influent-BOD of system effluent)/(TN of system influent-TN of system effluent), for conventional systemsA 2 In the case of the/O process, the nitrogen removal is mainly used and the delta BOD/delta TN is generally used>4, the general delta BOD/delta TN is adopted when the denitrification and dephosphorization effect is better>7 when Δ BOD/Δ TN<4 hours show that the system realizes TN removal with lower carbon source requirement;
the flow flux refers to the actual flow synthesis including water inflow and various refluxes during the actual operation of each partition in the reaction tank; for conventional A 2 In the/O process, if the inflow rate is Q1, the sludge reflux ratio is 100 percent, and the nitrifying liquid reflux ratio is 300 percent, the flow fluxes of the anaerobic zone, the anoxic zone and the aerobic zone are respectively 2Q1, 5Q1 and 5Q1, and the maximum flow flux is 5Q 1; according to the invention, if the inflow rate is Q2, the inflow rate of the pre-anoxic zone is 10% Q2, the inflow rate of the anaerobic zone is 90% Q2, the sludge reflux ratio is 100%, and the flow rate of the sludge surpassing pipe is 100% Q2, the flow rates of the pre-anoxic zone, the anaerobic zone, the intermediate sedimentation zone, the aerobic nitrification zone, the denitrification zone and the aerobic decarburization zone are respectively 1.1Q2, 2Q2, 2Q2, Q2, 2Q2 and 2Q2, and the maximum flow rate is 2Q 2;
the sludge age of the suspended sludge in the system is calculated according to the sludge concentration and the sludge discharge amount of the system without considering the sludge age of the suspended filler biomembrane part;
the phosphorus content of the sludge, namely the phosphorus content of the sludge in unit mass, is generally 3-6% in the biological phosphorus removal process if the biological phosphorus removal effect is good; for the tradition A 2 In the O process, the phosphorus content of the common sludge is 1.5 to 3.5 percent;
nitrification area load, i.e. the amount of ammonia nitrogen that can be oxidized per day, kgN/m, per unit surface area of biofilm 2 D; the nitrification area load of the aerobic nitrification area is the sum of the inflow rate x (system inflow ammonia nitrogen-system outflow ammonia nitrogen)/the surface area of the suspended carriers of the aerobic nitrification area;
organic area load, i.e. biofilm per surface area, the amount of BOD that can be oxidised per day, kgBOD/m 2 D, BOD both refer to BOD 5 The organic area load of the aerobic decarburization area is the sum of the inflow water flow rate x (1+ sludge reflux ratio) x (the inflow water BOD of the aerobic decarburization area-the outflow water BOD of the aerobic decarburization area)/the surface area of the suspended carrier of the aerobic decarburization area;
denitrification sludge load, i.e. the amount of nitrate capable of denitrification per day, kgN/kgMLSS/d, per unit mass of sludge; denitrification sludge load of the denitrification area, namely water inlet flow rate x (system water inlet TN-system water outlet TN)/(denitrification area pool capacity x denitrification area sludge concentration);
the influent C/N refers to system influent BOD/system influent TN, generally requires that the influent C/N is more than 4 for biological denitrification, the influent C/N is more than 7 for biological denitrification and dephosphorization, and the influent C/N of domestic general domestic sewage is generally less than 4, belongs to carbon source deficiency and needs external carbon source.
As well known by people in the industry, a pure membrane process, namely, microorganisms mainly grow in an attached state biofilm mode, and a small amount of suspended state microorganisms exist due to the fact that the biofilm is aged and shed in the process, and the concentration of general suspended state sludge is less than 0.5 g/L; the sludge membrane is compounded, namely microorganisms grow in an attached state biological membrane mode and a suspended state activated sludge mode at the same time, and the concentration of the suspended state sludge is more than 2.0 g/L.
The water inlet baffle (D1) of the pre-anoxic zone is arranged to fully mix the inlet water with the return sludge, quickly consume the nitrate carried in the return sludge and simultaneously prevent short flow in the pre-anoxic zone (PreA); the water inlet baffle (D2) of the denitrification area is arranged to fully mix the nitrified liquid and the overtaking sludge, quickly consume molecular dissolved oxygen carried in the nitrified liquid and prevent short flow in the denitrification Area (ANP); the water outlet zone (CS) is mainly used for stabilizing the water outlet liquid level and reducing the dissolved oxygen of the outlet water, and is not aerated or is aerated in a small amount by adopting a perforated pipe and is only used for stirring; between the intermediate settling zone (S1) and the aerobic nitrification zone (ON), water flow enters the aerobic nitrification zone (ON) through water drop and is mainly used for controlling the flux of the aerobic nitrification zone (ON); in order to prevent backflow sludge from quickly consuming VFA in the inlet water, only 10% -20% of Q of the flow of the branch inlet pipe (P2) enters a pre-anoxic zone (PreA), and most of the inlet water flow directly enters an anaerobic zone (AP); the bottom of the intermediate settling zone (S1) is provided with a mud bucket, and the bottom of the intermediate settling zone is inclined towards the mud bucket, so that the sludge settling and concentration are mainly enhanced, and the sludge concentration in the sludge surpassing pipe (P4) is improved; the maximum flux of each zone in the system is not more than 2.2Q, and the concentration conditions of high-concentration phosphate, nitrate and organic matters are mainly provided for a denitrification zone (ANP); the sludge age of the suspended sludge in the system is 4-12 days, and the sludge age is mainly controlled to be shortIs suitable for growth of phosphorus accumulating bacteria, while the traditional A 2 The general sludge age of the/O process is 15-25 d; sludge phosphorus content of return sludge>4 percent, the biological phosphorus removal effect in the system is good; the sludge concentration in the aerobic nitrification area (ON)<0.5g/L for limiting the suspended sludge to enter an aerobic nitrification area (ON); the DO of the aerobic nitrification area (ON) is 2.0-6.0mg/L, the nitrification condition is met, the nitrification load is gradually increased along with the increase of the DO, and the DO is adjusted according to the nitrification requirement condition in the system.
When the system is designed, the retention time of the anaerobic zone (AP) is 1.5 to 2.5 hours, the retention time of the pre-anoxic zone (PreA) is 0.5 to 1.0 hour, the retention time of the intermediate sedimentation zone (S1) is 1.5 to 3.0 hours, and the retention time of the water outlet zone (CS) is<0.5h, the retention time of the aerobic decarburization area (OC) is 0.5-2.0 h; the aerobic nitrification area (ON) is designed according to the nitrification area load, and the nitrification area load of the aerobic nitrification area (ON) is 0.0005-0.0015kgN/m 2 Determining the adding amount of the suspension carrier according to the surface area of the required suspension carrier and the effective specific surface area of the suspension filler, and determining the tank capacity according to the adding amount of the suspension carrier and the filling rate; because the nitrification of the system mainly occurs in an aerobic nitrification area (ON), when the nitrification area load is calculated, the sum of the inflow rate x (system inflow ammonia nitrogen-system outflow ammonia nitrogen)/the surface area of the suspended carriers in the aerobic nitrification area is calculated; the aerobic decarbonization area (OC) is designed according to the organic volume load, and the organic area load of the aerobic decarbonization area (OC) is 0.004-0.012kgBOD/m 2 Determining the addition amount of a suspension carrier according to the required surface area of the suspension carrier and the effective specific surface area of a suspension filler, determining the tank volume according to the addition amount of the suspension carrier and the filling rate, and calculating the sum of the water inlet flow rate x (1+ sludge reflux ratio) x (BOD of water inlet of an aerobic decarburization area-BOD of water outlet of the aerobic decarburization area)/the surface area of the suspension carrier of the aerobic decarburization area when calculating the organic area load, wherein the BOD of the water inlet of the aerobic decarburization area is generally 15-40mg/L, and the actual flow flux is considered; the denitrification Area (ANP) is designed according to the denitrification sludge load, the denitrification sludge load of the denitrification Area (ANP) is 0.03-0.06kgN/kgMLSS/d, and the tank volume is determined according to the sludge concentration; the related loads are all influenced by factors such as temperature, pH, DO, organic matters and the like; the filling rate of the suspension carrier is 30-60%, and the filling rate of the suspension carrier is too high, so that the tank capacity of an adding area can be enlarged, and the filling rate is reduced; suspension carrier fillingThe filling rate is too small, the tank volume of the feeding area can be reduced, and the filling rate is increased; if the system has the requirement of increasing the load in the future, the filling rate can be taken as the lower limit, and the filling rate is increased when the load is increased in the future; if the system has higher requirements for the occupied area, the filling rate can be limited to the upper limit.
The beneficial technical effects of the invention are as follows:
1) the high-efficiency denitrification and dephosphorization is much higher than that of the traditional process, wherein the TN removal rate is more than 80 percent, and the TP removal rate is more than 90 percent;
2) the operation is energy-saving, the maximum flow flux in the reaction tank is only 2.2Q, which is far lower than that of the traditional A 2 5Q of the O process and 15-25Q of the traditional oxidation ditch process; for the suspended filler area, because DO directly influences the nitrification load, DO can be flexibly adjusted according to the water inflow load, so that energy conservation and consumption reduction are realized;
3) the operation is low carbon, and the C/N of the inlet water required by removing nitrogen and phosphorus can be effectively reduced; when the traditional process can realize efficient nitrogen and phosphorus removal, the C/N of the inlet water is more than 7, and the invention can finish the efficient nitrogen and phosphorus removal when the C/N of the inlet water is less than 4;
4) the load is high, the occupied area is saved, the denitrification and dephosphorization microbial system is separated, the nitrification process depends on nitrifying floras on a suspension carrier in an aerobic nitrification area, the denitrification process and the dephosphorization process depend on suspended sludge, and the suspended sludge does not enter the aerobic nitrification area, so that the complete separation of autotrophic floras and heterotrophic floras is realized, the independent control is facilitated, respective optimal conditions are created for the respective floras, the treatment load is high, and the occupied area is reduced by 20-40% compared with the traditional process;
5) the denitrification dephosphorization is realized, areas with high phosphate, nitrate and organic matter concentration are created, and good conditions are created for the denitrification dephosphorization; in the traditional process, the total reflux is large, so that a high-concentration region is difficult to realize in a denitrification region; the invention effectively reduces the flux, can realize high matrix concentration, and the sludge in the anaerobic zone adsorbs a large amount of organic matters and directly enters the denitrification zone, thereby improving the utilization efficiency of the carbon source;
6) the removal rate of TN is not limited by the reflux ratio and the aerobic/non-aerobic ratio, the traditional A 2 the/O process supplies nitrate to the anoxic zone in a reflux manner, and generally has total reflux to ensure the continuous flow plug flow stateThe ratio is not more than 400%, and the TN removal rate is not more than 80% theoretically; the invention adopts a direct current mode to provide nitrate for the denitrification area, and the TN removal rate is not limited by the reflux ratio; tradition A 2 The O process considers the normal metabolism of nitrifying flora and requires aerobic HRT>The non-aerobic HRT realizes the flora separation, so that the system is not limited again;
7) the control is simple, the operation and management are easy and convenient, and compared with a double-sludge system, the single-stage biological system is simple to control; compared with a fixed filler, the operation and management are convenient, the dynamic biofilm is updated through the fluidization process of the suspended carrier, and the trouble of mud death or blockage is avoided.
Drawings
FIG. 1 is a schematic diagram of a process system of the present invention.
In the figure: s0 is a reaction tank, S2 is a secondary sedimentation tank, PreA is a pre-anoxic zone, AP is an anaerobic zone, S1 is a middle sedimentation zone, ON is an aerobic nitrification zone, ANP is a denitrification zone, OC is an aerobic decarburization zone, CS is a water outlet zone, P1 is a main water inlet pipe, P2 is a branch water inlet pipe, P3 is a water outlet pipe, P4 is a sludge overrun pipe, P5 is a sludge return pipe, P6 is a residual sludge discharge pipe, P7 is a connecting pipe, G1 is a pre-anoxic zone anaerobic zone partition wall, G2 is an anaerobic zone middle sedimentation zone partition wall, G3 is a middle sedimentation zone aerobic nitrification zone partition wall, G4 is an aerobic nitrification zone denitrification zone, G5 is a denitrification zone aerobic decarburization zone partition wall, G9 is an aerobic denitrification zone water outlet zone hole partition wall, K1 is a pre-anoxic zone hole, K56 is a sedimentation zone middle sedimentation zone aerobic denitrification zone partition wall, K6353 is an aerobic denitrification zone, K867 is an aerobic denitrification zone, K denitrification zone is an aerobic denitrification zone partition wall 867, w1 is a porous plate of a denitrification zone of an aerobic nitrification zone, W2 is a porous plate of a water outlet zone of an aerobic decarburization zone, D1 is a water inlet baffle of a pre-anoxic zone, D2 is a water inlet baffle of a denitrification zone, ND is a mud bucket, J1 is a stirrer of the pre-anoxic zone, J2 is a stirrer of an anaerobic zone, and J3 is a stirrer of the denitrification zone.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer and clearer, the present invention will be further described in detail with reference to specific embodiments.
The invention provides a low carbon-nitrogen ratio biological nitrogen and phosphorus removal method, which can solve the problems of low efficiency, high external carbon source dosage, large reflux ratio, increased energy consumption, difficulty in both nitrogen and phosphorus removal and the like of the traditional nitrogen and phosphorus removal process and is suitable for biological nitrogen and phosphorus removal of sewage and upgrading and reconstruction of a sewage treatment plant.
The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention. The invention, as shown in fig. 1, comprises a reaction tank (S0), a secondary sedimentation tank (S2) and a connecting pipeline; the reaction tank (S0) is sequentially provided with a pre-anoxic zone (PreA), an anaerobic zone (AP), a middle sedimentation zone (S1), an aerobic nitrification zone (ON), a denitrification zone (ANP), an aerobic decarburization zone (OC) and a water outlet zone (CS) from a water inlet end to a water outlet end; the pre-anoxic zone (PreA), the anaerobic zone (AP) and the denitrification zone (ANP) are provided with stirrers; a mud bucket (ND) is arranged at the bottom of the middle sinking area (S1), and the bottom of the middle sinking area (S1) slopes towards the mud bucket (ND) with the slope of 1% -3%; the aerobic nitrification area (ON) and the aerobic decarbonization area (OC) are provided with aeration; suspension carriers are added into the aerobic nitrification area (ON) and the aerobic decarbonization area (OC); the density of the suspension carrier is 0.90-0.98g/cm 3 Void fraction>85 percent, the filling rate is 30 to 60 percent, and the specific surface area is more than or equal to 300m 2 /m 3 (ii) a The pre-anoxic zone (PreA) is communicated with the anaerobic zone (AP) through a pre-anoxic zone hole (K1) arranged on a pre-anoxic zone partition wall (G1); the anaerobic zone (AP) is communicated with the intermediate settling zone (S1) through intermediate settling zone holes (K2) arranged on an intermediate settling zone partition wall (G2) of the anaerobic zone; the middle sedimentation zone (S1) is communicated with the aerobic nitrification zone (ON) through a middle sedimentation zone aerobic nitrification zone hole (K3) arranged ON a middle sedimentation zone aerobic nitrification zone partition wall (G3); the aerobic nitrification region (ON) is communicated with the denitrification region (ANP) through an aerobic nitrification region denitrification region hole (K4) arranged ON an aerobic nitrification region denitrification region partition wall (G4); a porous plate (W1) of the denitrification area of the aerobic nitrification area is arranged on the hole (K4) of the denitrification area of the aerobic nitrification area; the denitrification Area (ANP) is communicated with the aerobic decarbonization area (OC) through denitrification area aerobic decarbonization area holes (K5) arranged on a denitrification area aerobic decarbonization area partition wall (G5); the aerobic decarburization area (OC) is communicated with the water outlet area (CS) through water outlet area holes (K6) of the aerobic decarburization area arranged on the water outlet area partition wall (G6) of the aerobic decarburization area; the holes (K6) of the water outlet zone of the aerobic decarburization zone are provided with a plurality of water outlet zones of the aerobic decarburization zoneAn orifice plate (W2); the upper edge of the hole (K1) of the anaerobic zone of the pre-anoxic zone is 0.5m-1.5m below the water surface of the anaerobic zone (AP); the distance between the center of the settling zone hole (K2) in the anaerobic zone and the bottom of the tank is 50-60% of the effective water depth of the anaerobic zone (AP); the distance from the lower edge of the aerobic nitrification area hole (K3) of the intermediate sedimentation area to the bottom of the tank is the same as the effective water depth of the anaerobic Area (AP); the upper edge of the hole (K4) of the denitrification area of the aerobic nitrification area is 0.5m-1.5m below the water surface of the denitrification Area (ANP); the upper edge of the hole (K5) of the aerobic decarburization area of the denitrification area is 0.5-1.5 m below the water surface of the denitrification Area (ANP); the upper edge of the hole (K6) of the water outlet zone of the aerobic decarbonization zone is 0.5m-1.5m below the water surface of the denitrification zone (ANP); the connecting pipeline comprises a main water inlet pipe (P1), a branch water inlet pipe (P2), a water outlet pipe (P3), a sludge overrunning pipe (P4), a sludge return pipe (P5), a residual sludge discharge pipe (P6) and a connecting pipe (P7); the main water inlet pipe (P1) is communicated with the bottom of the front end of the anaerobic zone (AP); one end of the branch water inlet pipe (P2) is communicated with the middle part of the front end of the pre-anoxic zone (PreA), and the other end is communicated with the main water inlet pipe (P1); one end of the sludge surpassing pipe (P4) is communicated with a sludge hopper (ND) at the bottom of the intermediate settling zone (S1), and the other end is communicated with the bottom of the front end of the denitrification zone (ANP); one end of the sludge return pipe (P5) is communicated with the bottom of the secondary sedimentation tank (S2), and the other end is communicated with the middle part of the front end of the pre-anoxic zone (PreA); the residual sludge discharge pipe (P6) is communicated with the bottom of the secondary sedimentation tank (S2); the water outlet area (CS) is communicated with the secondary sedimentation tank (S2) through a connecting pipe (P7); the water outlet pipe (P3) is communicated with the top of the secondary sedimentation tank (S2); the sludge surpassing pipe (P4) and the sludge return pipe (P5) are respectively provided with a sludge pump; the front end of the pre-anoxic zone (PreA) is provided with a pre-anoxic zone water inlet baffle (D1), the top end of the pre-anoxic zone water inlet baffle (D1) is 0.5m-1.0m above the water surface of the anaerobic zone (AP), and the bottom end of the pre-anoxic zone water inlet baffle (D1) is 0.5m-1.0m above the bottom of the anaerobic zone (AP); the front end of the denitrification Area (ANP) is provided with a denitrification area water inlet baffle (D2), the top end of the denitrification area water inlet baffle (D2) is 0.5-1.0 m above the water surface of the denitrification Area (ANP), and the bottom end of the denitrification area water inlet baffle (D2) is 0.5-1.0 m above the bottom of the denitrification Area (ANP); the water level elevations of the pre-anoxic zone (PreA), the anaerobic zone (AP) and the intermediate settling zone (S1) are the same; the water surface elevations of the aerobic nitrification area (ON), the denitrification Area (ANP), the aerobic decarburization area (OC) and the water outlet area (CS) are the same; denitrification of water surface elevation ratio in anaerobic zone (AP)The water surface of the chemical Area (ANP) is 0.1-0.3m higher.
Part of the inlet water enters the pre-anoxic zone (PreA) through a branch inlet pipe (P2), and part of the inlet water directly enters the anaerobic zone (AP) through a main inlet pipe (P1); the return sludge is returned to the pre-anoxic zone (PreA) from the secondary sedimentation tank (S2) by the sludge return pipe (P5), and is rapidly mixed with the inlet water of the branch water inlet pipe (P2) in front of the water inlet baffle plate (D1) of the pre-anoxic zone; the mud-water mixture in the pre-anoxic zone (PreA) enters the anaerobic zone (AP) through the holes (K1) of the anaerobic zone in the pre-anoxic zone; sludge-water mixture in the anaerobic zone (AP) enters a middle sedimentation zone (S1) through a middle sedimentation zone hole (K2) in the anaerobic zone, sludge-water separation is realized after sedimentation, supernatant enters an aerobic nitrification zone (ON) through a middle sedimentation zone aerobic nitrification zone hole (K3) drop water, and settled sludge enters a sludge hopper (ND) and then directly enters the bottom of the front end of a denitrification zone (ANP) through a sludge overrunning pipe (P4); water in the aerobic nitrification region (ON) enters the front end of the denitrification region (ANP) through an aerobic nitrification region denitrification region perforated plate (W1) arranged ON an aerobic nitrification region denitrification region hole (K4), and is mixed with sludge surpassed through a sludge surpassing pipe (P4) in front of a denitrification region water inlet baffle plate (D2); the mud-water mixture in the denitrification Area (ANP) enters an aerobic decarburization area (OC) through holes (K5) in the aerobic decarburization area of the denitrification area; the mud-water mixture in the aerobic decarbonization zone (OC) enters the water outlet zone (CS) through an aerobic decarbonization zone water outlet zone porous plate (W2) arranged on an aerobic decarbonization zone water outlet zone hole (K6), flows into the secondary sedimentation tank (S2) from the water outlet zone (CS) through a connecting pipe (P7), and finally the treated effluent is discharged from a water outlet pipe (P3) of the secondary sedimentation tank (S2).
Example 1:
the sewage flow Q is 100000m 3 The average value of inlet water is 45mg/L, TN55mg/L, TP6mg/L, BOD160mg/L, and the standard of outlet water is ammonia nitrogen for domestic sewage<3mg/L、TN<10mg/L、TP<0.5mg/L、BOD<10mg/L, influent BOD/TN =2.91, using the apparatus described in FIG. 1.
The retention time of the pre-anoxic zone (PreA) is 0.5h, the retention time of the anaerobic zone (AP) is 2.0h, the retention time of the intermediate sedimentation zone (S1) is 2.5h, and the retention time of the water outlet zone (CS) is 0.5 h; the retention time of an aerobic nitrification region (ON) is 2.5h, and the specific surface area is 800m 2 /m 3 Suspension carrier, filling rate 50%; aerobic decarbonization zone (OC) residenceThe time is 0.5h, and the specific surface area is 800m 2 /m 3 Suspension carrier, filling rate 30%; the residence time of the denitrification zone (ANP) is 4.5 h; the total residence time was 13.0 h.
The sludge concentration of the aerobic nitrification area (ON) is 0.3g/L, the sludge concentration of the anaerobic Area (AP), the denitrification Area (ANP), the aerobic decarburization area (OC) and the water outlet area (CS) is 4-4.5g/L, and the sludge age of the suspended sludge in the system is 6-8 d. The flow rate of the main water inlet pipe (P1) is 80-90% Q, the flow rate of the sludge return pipe (P5) is 70-90% Q, and the flow rate of the sludge surpassing pipe (P4) is 70-90% Q; the DO of the aerobic nitrification area (ON) is 2.0-6.0mg/L, the DO of the aerobic decarbonization area (OC) is 1.5-4.5mg/L, and the DO of the water outlet area (CS) is 1.0-3.0 mg/L.
The maximum flux of each area in the system is 1.9Q; the phosphorus content of the sludge of the return sludge is 4.8 percent.
The average value of the TN of the effluent is 8.2mg/L, the average value of the TP of the effluent is 0.4mg/L, the average value of BOD of the effluent is 6mg/L, the TP removal rate = (6-0.4)/6=93.3% >90%, and Δ BOD/Δ TN = (160-6)/(55-8.2) = 3.29.
Although terms such as denitrification zone, sludge return line, sludge override line, etc. are used more often herein, the possibility of using other terms is not excluded, and simple substitutions of these terms by those skilled in the art in light of the present disclosure are intended to be within the scope of the present invention. The parts which are not described in the above modes can be realized by adopting or referring to the prior art. The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, it should be noted that, for those skilled in the art, many modifications and decorations can be made without departing from the technical principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (3)
1. A biological nitrogen and phosphorus removal method with a low carbon-nitrogen ratio is characterized in that an adopted system consists of a reaction tank (S0), a secondary sedimentation tank (S2) and a connecting pipeline, and inlet water sequentially passes through the reaction tank (S0) and the secondary sedimentation tank (S2) to remove pollutants; the reaction tank (S0) is sequentially provided with a pre-anoxic zone (PreA), an anaerobic zone (AP), a middle sedimentation zone (S1), an aerobic nitrification zone (ON), a denitrification zone (ANP) from a water inlet end to a water outlet end,An aerobic decarbonization zone (OC) and a water outlet zone (CS); the aerobic nitrification area (ON) and the aerobic decarbonization area (OC) are provided with aeration; suspension carriers are added into the aerobic nitrification area (ON) and the aerobic decarbonization area (OC); the density of the suspension carrier is 0.90-0.98g/cm 3 Void fraction>85 percent, the filling rate is between 30 and 60 percent, and the specific surface area is more than or equal to 300m 2 /m 3 (ii) a The pre-anoxic zone (PreA) is communicated with the anaerobic zone (AP) through a pre-anoxic zone hole (K1) arranged on a pre-anoxic zone partition wall (G1); the anaerobic zone (AP) is communicated with the intermediate settling zone (S1) through intermediate settling zone holes (K2) arranged on an intermediate settling zone partition wall (G2) of the anaerobic zone; the middle sedimentation zone (S1) is communicated with the aerobic nitrification zone (ON) through a middle sedimentation zone aerobic nitrification zone hole (K3) arranged ON a middle sedimentation zone aerobic nitrification zone partition wall (G3); the aerobic nitrification region (ON) is communicated with the denitrification region (ANP) through an aerobic nitrification region denitrification region hole (K4) arranged ON an aerobic nitrification region denitrification region partition wall (G4); a porous plate (W1) of the denitrification area of the aerobic nitrification area is arranged on the hole (K4) of the denitrification area of the aerobic nitrification area; the denitrification Area (ANP) is communicated with the aerobic decarbonization area (OC) through denitrification area aerobic decarbonization area holes (K5) arranged on a denitrification area aerobic decarbonization area partition wall (G5); the aerobic decarburization area (OC) is communicated with the water outlet area (CS) through water outlet area holes (K6) of the aerobic decarburization area arranged on the water outlet area partition wall (G6) of the aerobic decarburization area; the aerobic decarbonization zone water outlet zone porous plate (W2) is arranged on the aerobic decarbonization zone water outlet zone hole (K6);
the connecting pipeline comprises a main water inlet pipe (P1), a branch water inlet pipe (P2), a water outlet pipe (P3), a sludge overrunning pipe (P4), a sludge return pipe (P5), a residual sludge discharge pipe (P6) and a connecting pipe (P7); the main water inlet pipe (P1) is communicated with the bottom of the front end of the anaerobic zone (AP); one end of the branch water inlet pipe (P2) is communicated with the middle part of the front end of the pre-anoxic zone (PreA), and the other end is communicated with the main water inlet pipe (P1); one end of the sludge surpassing pipe (P4) is communicated with a sludge hopper (ND) at the bottom of the intermediate settling zone (S1), and the other end is communicated with the bottom of the front end of the denitrification zone (ANP); one end of the sludge return pipe (P5) is communicated with the bottom of the secondary sedimentation tank (S2), and the other end is communicated with the middle part of the front end of the pre-anoxic zone (PreA); the residual sludge discharge pipe (P6) is communicated with the bottom of the secondary sedimentation tank (S2); the water outlet area (CS) is communicated with the secondary sedimentation tank (S2) through a connecting pipe (P7);
the method comprises the following steps:
part of the inlet water enters the pre-anoxic zone (PreA) through a branch inlet pipe (P2), and part of the inlet water directly enters the anaerobic zone (AP) through a main inlet pipe (P1); the return sludge is returned to the pre-anoxic zone (PreA) from the secondary sedimentation tank (S2) by the sludge return pipe (P5), and is rapidly mixed with the inlet water of the branch water inlet pipe (P2) in front of the water inlet baffle plate (D1) of the pre-anoxic zone; the mud-water mixture in the pre-anoxic zone (PreA) enters the anaerobic zone (AP) through the holes (K1) of the anaerobic zone in the pre-anoxic zone; sludge-water mixture in the anaerobic zone (AP) enters a middle sedimentation zone (S1) through a middle sedimentation zone hole (K2) in the anaerobic zone, sludge-water separation is realized after sedimentation, supernatant enters an aerobic nitrification zone (ON) through a middle sedimentation zone aerobic nitrification zone hole (K3) drop water, and settled sludge enters a sludge hopper (ND) and then directly enters the bottom of the front end of a denitrification zone (ANP) through a sludge overrunning pipe (P4); water in the aerobic nitrification region (ON) enters the front end of the denitrification region (ANP) through an aerobic nitrification region denitrification region perforated plate (W1) arranged ON an aerobic nitrification region denitrification region hole (K4), and is mixed with sludge surpassed through a sludge surpassing pipe (P4) in front of a denitrification region water inlet baffle plate (D2); the sludge-water mixture obtained in the denitrification Area (ANP) enters an aerobic decarbonization area (OC) through holes (K5) in the aerobic decarbonization area of the denitrification area; the mud-water mixture obtained in the aerobic decarbonization zone (OC) enters a water outlet zone (CS) through an aerobic decarbonization zone water outlet zone porous plate (W2) arranged on a hole (K6) of the aerobic decarbonization zone water outlet zone, flows into a secondary sedimentation tank (S2) from the water outlet zone (CS) through a connecting pipe (P7), and finally, the treated effluent is discharged from a water outlet pipe (P3) of the secondary sedimentation tank (S2);
in the method, the retention time of the inflow water in the pre-anoxic zone (PreA) is 0.5 to 1.0 hour, the retention time in the anaerobic zone (AP) is 1.5 to 2.5 hours, the retention time in the intermediate settling zone (S1) is 1.5 to 3.0 hours, the retention time in the aerobic decarburization zone (OC) is 0.5 to 2.0 hours, and the retention time in the effluent zone (CS) is less than or equal to 0.5 hour;
the sludge concentration of the aerobic nitrification area (ON) is less than 0.5g/L, and the sludge concentration of the anaerobic Area (AP), the denitrification Area (ANP), the aerobic decarburization area (OC) and the water outlet area (CS) is 3-8 g/L; the sludge age of the suspended sludge in the system is 4-12 d;
the DO of the aerobic nitrification zone (ON) is 2.0-6.0mg/L, the DO of the aerobic decarbonization zone (OC) is 1.5-4.5mg/L, and the DO of the water outlet zone (CS) is 1.0-3.0 mg/L;
when the inflow water flow is Q, the flow of the main water inlet pipe (P1) is 80-90% Q, the flow of the sludge return pipe (P5) is 30-120% Q, and the flow of the sludge surpassing pipe (P4) is 85-100% of the flow of the sludge return pipe (P5);
the retention time of the aerobic nitrification region (ON) is determined according to the nitrification area load of the aerobic nitrification region (ON), and the nitrification area load of the aerobic nitrification region (ON) is 0.0005-0.0015kgN/m 2 D; the retention time of the aerobic decarbonization area (OC) is determined according to the organic area load of the aerobic decarbonization area (OC), and the organic area load of the aerobic decarbonization area (OC) is 0.004-0.012kgBOD/m 2 D; the retention time of the denitrification Area (ANP) is determined according to the denitrification sludge load of the denitrification Area (ANP), and the denitrification sludge load of the denitrification Area (ANP) is 0.03-0.06 kgN/kgMLSS/d.
2. The method of claim 1, wherein when the ammonia nitrogen at the outlet of the aerobic nitrification zone (ON) is less than 1.5mg/L, the DO is reduced by no more than 15% each time, and the adjustment interval is at least 4h each time; when the ammonia nitrogen at the water outlet end of the aerobic nitrification area (ON) is more than 3mg/L, the DO is increased, the increase is not more than 15% every time, and the adjustment interval is at least 4h every time.
3. The method of claim 1, wherein the removal rate of TP is greater than 90% or the effluent TP is less than 1mg/L, Δ BOD/Δ TN is less than 4; the maximum flux of each area in the system does not exceed 2.2Q; the sludge phosphorus content of the return sludge is more than 4 percent.
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