CN108483654A

CN108483654A - A kind of double mode sewerage nitrogen and phosphor processing system and method

Info

Publication number: CN108483654A
Application number: CN201810546935.8A
Authority: CN
Inventors: 王金龙; 李德祥; 其他发明人请求不公开姓名
Original assignee: Individual
Current assignee: Individual
Priority date: 2018-06-01
Filing date: 2018-06-01
Publication date: 2018-09-04

Abstract

The present invention discloses a kind of double mode sewerage nitrogen and phosphor processing system and method, belongs to sewage treatment field.Sewage of the present invention passes sequentially through reaction tank, secondary settling tank, realizes intensified denitrification and dephosphorization, when using surmounting sludge operational mode, total tp removal rate>90% or water outlet TP<1mg/L, Δ BOD/ Δs TN<The area 4, system Nei Ge maximum stream flow flux is no more than 2.2Q, the sludge phosphorus content of returned sludge>4%, have many advantages, such as that high-efficient denitrification and dephosphorization, energy saving in running low-carbon, load are high, take up an area province, realization denitrification dephosphorization, TN removal rates are not limited by reflux ratio, it is convenient to control simple operation management.The system of the present invention is made of reaction tank, secondary settling tank and connecting line, reaction tank is followed successively by pre- anoxic zone, anaerobic zone, the areas Zhong Chen, aerobic nitrification area, denitrification zone, aerobic decarburization area, exhalant region from water inlet end to water outlet, connecting line includes that main water inlet tube, branch's water inlet pipe, outlet pipe, sludge surmount pipe, mud return line, excess sludge delivery pipe etc., and technological process is simple.

Description

A kind of double mode sewerage nitrogen and phosphor processing system and method

Technical field

The invention belongs to technical field of sewage, and in particular to a kind of double mode sewerage nitrogen and phosphor processing system and method.

Background technology

Biochemical wastewater treatment is based on traditional denitrogenation dephosphorizing mechanism more.Denitrification process, including nitrification, denitrification； Nitrification, i.e. Autotrophic nitrification bacterium（AOB、NOB）Under aerobic condition, NH₄ ⁺-N→NO₂ ^--N→NO₂ ^--N；Denitrification, I.e. denitrification flora under anoxic conditions, with NO_X ^-It is electron donor, NO for electron acceptor, organic matter₃ ^--N→NO₂ ^--N→N₂。 Biological Phosphorus Removal Process, including anaerobic phosphorus release, aerobic transition inhale phosphorus, discharge excess sludge realizes biological phosphate-eliminating；In anaerobic processes, gather Phosphorus bacterium absorbs organic matter and is stored in cell body, discharges phosphate；It is organic by being stored in dissolved oxygen oxidative cell when aerobic Object absorbs the phosphorus in water body.As it can be seen that for denitrogenation dephosphorizing, core includes three classes flora, nitrifying bacteria community, denitrification flora, poly- phosphorus Flora.Nitrifying bacteria community belongs to autotrophic bacterium, and stringent aerobic, specific growth rate is low；Most of denitrification flora belongs to heterotrophic bacteria, than life Long rate is high；PolyP bacteria belongs to facultative heterotrophic bacteria, and specific growth rate is high.At present in the typical treatment process of sewage plant, work is mostly used Property sludge and according to A²It is/O technology arrangements, i.e. anaerobism, anoxic, three sections aerobic, and flow back and nitrify to anoxic section in aerobic end Liquid provides nitrate for denitrification, other techniques are mostly to be based on A²The deformation technique of/O.

Typical A²There are following intrinsic shortcomings for/O techniques：

1）There are the contradiction on sludge age, denitrification flora, polyP bacteria groups, and short sludge age, nitrifying bacteria community to be needed to need to grow for denitrogenation dephosphorizing Sludge age, but only single sludge age in system, it is practical using compromise way, take into account denitrogenation dephosphorizing；But for nitrifying bacteria community, sludge age is not Foot, winter treatment effect is undesirable, and treatment effect is unstable when water inlet is fluctuated；For denitrification flora, polyP bacteria group, sludge age mistake Long, sludge has aging tendency, treatment effeciency to decline；

2）There are the difference in dissolved oxygen demand, polyP bacteria anaerobic phosphorus releases to need absolute anaerobism, the presence of dissolved oxygen for denitrogenation dephosphorizing It can influence even to inhibit anaerobic phosphorus release process, only anaerobic phosphorus release is more abundant, and aerobic stage could excessively inhale phosphorus, realizes good Biological phosphate-eliminating；The essence of denitrification process is denitrifying bacterium with NO_x ^-It is electron donor for electron acceptor, organic matter, if in the presence of Molecular state dissolved oxygen, then molecular state dissolved oxygen then can by preferentially be used as electron acceptor, be influenced denitrification efficiency；Nitrifying bacteria community is tight Lattice aerobic, detesting can be suppressed in the presence of anoxic and carbon source, therefore the HRT of aerobic section is greater than other process sections in traditional handicraft The synthesis of HRT, to ensure the analytic metabolism of nitrifying bacteria community；For activated sludge process, activated sludge is hybrid system, passes through each work Each function is realized in the separation of skill section, but still is restricted each other, including the arrangement spatially of each process section and the design etc. of HRT；

3）There are the contention in carbon source, polyP bacterias can only utilize the volatile fatty acid in organic matter, other forms for denitrogenation dephosphorizing Organic matter need first to be hydrolyzed into volatile fatty acid, could be utilized by polyP bacteria；Requirement of the denitrification flora to carbon source is slightly lower In polyP bacteria, but low-carbon organic matter can only be also utilized, there are the contentions of carbon source quality and quantity between denitrification flora and polyP bacteria group； General to require, biological denitrificaion requires water inlet C/N>4, water inlet C/N is required when biological carbon and phosphorous removal>7, and domestic general sanitary sewage C/N of intaking is universal<4, belong to carbon source deficiency, needs outer throwing carbon source；Nitrifying bacteria community is autotrophy, does not need organic carbon source, and organic Carbon source can generate nitrifying bacteria community the inhibition of metabolism when being more than a certain amount of.

The essence of denitrification process is with NO_X ^-It is electron donor for electron acceptor, organic matter；The sheet of polyP bacteria aerobic phosphorus absorption It is electron acceptor, organic matter for electron donor that matter, which is using oxygen,；If polyP bacteria can be with NO_X ^-It is electronics for electron acceptor, organic matter " carbon is dual-purpose ", denitrification dephosphorization then can be achieved in donor, reduces water inlet C/N demands, reduces the carbon source consumption of sewage disposal；And The research of molecular biology, it was found that this denitrification dephosphorization phenomenon is that this path denitrogenation dephosphorizing is laid a good foundation, and passes through height The creation of concentration phosphate, nitrate, organic substance environment can promote Denitrifying Phosphorus Removal to generate.

In addition, by the isometric sludge age flora of nitrifying bacteria community, detach, realizes with the short sludge age flora such as denitrification flora, polyP bacteria Sludge age detaches.Method of strain separating, including driving by double-energy, addition biomembrane etc..Driving by double-energy, i.e. two sets of biosystems, point Long sludge age and short sludge age flora are not carried, and system structure is complicated, and control difficulty is big, requires operational management high, it is difficult in engineering Middle large-area applications.In traditional A²Increase biomembrane in/O, fixed filler such as is installed in aerobic zone, but normal aeration provides Hydraulic shear be not enough to promote the normal update of microorganism on fixed filler, longtime running generates the areas Si Ni, serious to reduce Nitrification efficiency；If in traditional A²Suspending carrier is loaded in/O, although foring mud membrane compound technology, can not be removed for denitrification Phosphorus creates conditions, and suspending carrier system, when suspended state sludge concentration is excessive in system, the meeting of suspended state sludge and suspending carrier On biomembrane generate competition, reduce nitrification efficiency.

While it is noted that although utilization of carbon source rate can be improved in denitrification dephosphorization, but when C/N of intaking is increased, The consumption of its carbon source has limitation, may lead to have excessive organic matter to flow into nitrification region, influence system nitrification function；But it sets If timing considers nitrification design when C/N high, nitrification region pool capacity is necessarily will increase, it is uneconomical to improve cost；If can be in nitre Change in region, according to the difference of water inlet C/N and nitrification effect, pure membrane process and mud membrane compound technology is adjusted flexibly, you can ensures Treatment effect can also reduce investment, improve operational efficiency.

Invention content

Based on above-mentioned technical problem, a kind of double mode sewerage nitrogen and phosphor processing system of present invention offer and method.

The adopted technical solution is that：

A kind of double mode sewerage nitrogen and phosphor processing system, which is characterized in that system is by reaction tank (S0), secondary settling tank (S2) and connecting tube Road forms；Reaction tank (S0) from water inlet end to water outlet be followed successively by pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1), Aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS).

Preferably, the pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP), the areas Zhong Chen (S1) are equipped with and stir Mix device；The areas Zhong Chen (S1) bottom is equipped with bucket (ND), and the areas Zhong Chen (S1) bottom slope aspect bucket (ND), the gradient is in 1%-3%；Institute It states aerobic nitrification area (ON), aerobic decarburization area (OC) and is equipped with aeration；The aerobic nitrification area (ON) and aerobic decarburization area (OC) Add suspending carrier；The suspending vehicle density is 0.90-0.98g/cm³, voidage>85%, filling rate in 10%-60%, than Surface area >=300m²/m³。

Preferably, the pre- anoxic zone (PreA) and anaerobic zone (AP) are equipped with by pre- anoxic zone anaerobic zone partition wall (G1) Pre- anoxic zone anaerobic zone hole (K1) communicate；The anaerobic zone (AP) and the areas Zhong Chen (S1) separate wall by sinking in anaerobic zone (G2) the anaerobic zone areas the Zhong Chen hole (K2) being equipped with communicates；The areas Zhong Chen (S1) and aerobic nitrification zone (ON) pass through the areas Zhong Chen Aerobic nitrification separates aerobic nitrification area of the areas the Zhong Chen hole (K3) that wall (G3) is equipped with and communicates；The aerobic nitrification area (ON) and anti- Aerobic nitrification area denitrification zone hole (K4) phase that nitrification zone (ANP) is equipped with by aerobic nitrification area denitrification zone partition wall (G4) It is logical；Aerobic nitrification area denitrification zone hole (K4) is equipped with aerobic nitrification area denitrification zone porous plate (W1)；The anti-nitre Change area (ANP) and aerobic decarburization area (OC) and separates that denitrification zone that wall (G5) is equipped with is aerobic to be taken off by the aerobic decarburization in denitrification zone Carbon area hole (K5) communicates；The aerobic decarburization area (OC) and exhalant region (CS) pass through on aerobic decarburization area exhalant region partition wall (G6) The aerobic decarburization area exhalant region hole (K6) being equipped with communicates；The aerobic decarburization area exhalant region hole (K6) is equipped with aerobic decarburization Area's exhalant region porous plate (W2)；

The upper edge of the pre- anoxic zone anaerobic zone hole (K1) 0.5m-1.5m below anaerobic zone (AP) water surface；The anaerobic zone The centre-to-centre spacing bottom of pond distance of the areas Zhong Chen hole (K2) is the 50-60% of anaerobic zone (AP) available depth；The areas Zhong Chen aerobic nitrification The lower edge of area's hole (K3) is identical as anaerobic zone (AP) available depth away from bottom of pond distance；Aerobic nitrification area denitrification zone hole (K4) upper edge 0.5m-1.5m below denitrification zone (ANP) low liquid level (L) water surface；The aerobic decarburization area in denitrification zone hole The upper edge in hole (K5) 0.5m-1.5m below denitrification zone (ANP) low liquid level (L) water surface；The aerobic decarburization area exhalant region hole The upper edge in hole (K6) 0.5m-1.5m below denitrification zone (ANP) low liquid level (L) water surface.

Preferably, the connecting line includes that main water inlet tube (P1), branch's water inlet pipe (P2), outlet pipe (P3), sludge are super More manage (P4), mud return line (P5), excess sludge delivery pipe (P6), low liquid level connecting tube (P7), high liquid level connecting tube (P8)； The main water inlet tube (P1) communicates with anaerobic zone (AP) front bottom end；Described branch's water inlet pipe one end (P2) and pre- anoxic zone (PreA) front center communicates, and the other end is communicated with main water inlet tube (P1)；The sludge surmounts pipe one end (P4) and the areas Zhong Chen (S1) bucket (ND) of bottom communicates, and the other end is communicated with the front bottom end of denitrification zone (ANP)；The mud return line (P5) One end is communicated with the bottom secondary settling tank (S2), and the other end is communicated with pre- anoxic zone (PreA) front center；The excess sludge discharge Pipe (P6) is communicated with the bottom secondary settling tank (S2)；Exhalant region (CS) passes through low liquid level connecting tube (P7), height respectively with secondary settling tank (S2) Liquid level connecting tube (P8) communicates；It is communicated at the top of the outlet pipe (P3) and secondary settling tank (S2)；Sludge surmounts pipe (P4) and sludge returns Flow tube (P5) is respectively equipped with sludge pump；The low liquid level connecting tube center (P7) is identical as low liquid level (L) absolute altitude；High liquid level connecting tube (P8) center is identical as high liquid level (H) absolute altitude.

Preferably, pre- anoxic zone (PreA) front end is equipped with pre- anoxic zone inlet damper (D1), pre- anoxic zone water inlet gear The plate top (D1) is in the above 0.5m-1.0m of anaerobic zone (AP) water surface, and the pre- anoxic zone inlet damper bottom end (D1) is at anaerobic zone (AP) The above 0.5m-1.0m of bottom of pond；Denitrification zone (ANP) front end is equipped with denitrification zone inlet damper (D2), denitrification zone water inlet The baffle top (D2) is at denitrification zone (ANP) high liquid level (H) the above 0.5m-1.0m of the water surface, the bottom denitrification zone inlet damper (D2) End is in the above 0.5m-1.0m of denitrification zone (ANP) bottom of pond.

Preferably, the pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1) water surface absolute altitude are identical, with high liquid level (H) absolute altitude is identical；The aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) water surface mark It is high identical, there are two high liquid level (H), low liquid level (L) water surface absolute altitudes；High liquid level (H) absolute altitude is bigger 0.2- than low liquid level (L) absolute altitude 0.4m。

A kind of double mode sewerage nitrogen and phosphor processing method, using above system, which is characterized in that water inlet passes sequentially through system Reaction tank (S0), secondary settling tank (S2), realize the removal of pollutant；The system comprises surmount sludge operational mode and reflux nitrification Liquid operational mode；

Described to surmount sludge operational mode, a water inlet part enters pre- anoxic zone (PreA) by branch's water inlet pipe (P2), one Divide and anaerobic zone (AP) is directly entered by main water inlet tube (P1)；Mud return line (P5) flows back returned sludge from secondary settling tank (S2) Enter pre- anoxic zone (PreA), and is quickly mixed before pre- anoxic zone inlet damper (D1) with the water inlet of branch's water inlet pipe (P2)；In advance Mud mixture in anoxic zone (PreA) enters anaerobic zone (AP) by pre- anoxic zone anaerobic zone hole (K1)；Anaerobic zone (AP) Interior mud mixture enters the areas Zhong Chen (S1) by the anaerobic zone areas Zhong Chen hole (K2), and after precipitation, supernatant sinks in passing through Aerobic nitrification area of area hole (K3) drop enters aerobic nitrification area (ON), and the sludge of sedimentation enters super by sludge after bucket (ND) More pipe (P4) is directly entered denitrification zone (ANP) front bottom end；Water in aerobic nitrification area (ON) passes through the anti-nitre in aerobic nitrification area Change the aerobic nitrification area denitrification zone porous plate (W1) that area's hole (K4) is equipped with and enter the front end denitrification zone (ANP), and anti- Before nitrification zone inlet damper (D2) with the sludge that pipe (P4) surmounts surmounted by sludge mix；The muddy water of denitrification zone (ANP) is mixed It closes object and aerobic decarburization area (OC) is entered by the aerobic decarburization area hole (K5) in denitrification zone；The muddy water of aerobic decarburization area (OC) mixes The aerobic decarburization area exhalant region porous plate (W2) that object is equipped with by aerobic decarburization area exhalant region hole (K6), into exhalant region (CS), secondary settling tank (S2) is flowed into from exhalant region (CS) through low liquid level connecting tube (P7), it is finally processed to be discharged from secondary settling tank (S2) outlet pipe (P3) discharge；Pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP) blender are opened；It is aerobic Nitrification zone (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) are in low liquid level (L) operation；Sludge surmounts Pipe (P4) water (flow) direction flows to denitrification zone (ANP) by the areas Zhong Chen (S1)；

The reflux nitrification liquid operational mode, a water inlet part enter pre- anoxic zone (PreA) by branch's water inlet pipe (P2), and one Part is directly entered anaerobic zone (AP) by main water inlet tube (P1)；Mud return line (P5) returns returned sludge from secondary settling tank (S2) Pre- anoxic zone (PreA) is flowed into, and is quickly mixed before pre- anoxic zone inlet damper (D1) with the water inlet of branch's water inlet pipe (P2)； Mud mixture in pre- anoxic zone (PreA) enters anaerobic zone (AP) by pre- anoxic zone anaerobic zone hole (K1)；Anaerobic zone (AP) interior mud mixture enters the areas Zhong Chen (S1) by the anaerobic zone areas Zhong Chen hole (K2)；Muddy water mixing in the areas Zhong Chen (S1) Object enters aerobic nitrification area (ON) by aerobic nitrification area of the areas Zhong Chen hole (K3)；Mud mixture in aerobic nitrification area (ON) Enter denitrification by the aerobic nitrification area denitrification zone porous plate (W1) that aerobic nitrification area denitrification zone hole (K4) is equipped with The front end area (ANP)；A mud mixture part for denitrification zone (ANP) surmounts pipe (P4) by sludge and is back to the areas Zhong Chen (S1) At bucket (ND), a part enters aerobic decarburization area (OC) by the aerobic decarburization area hole (K5) in denitrification zone；Aerobic decarburization area (OC) the aerobic decarburization area exhalant region porous plate that mud mixture is equipped with by aerobic decarburization area exhalant region hole (K6) (W2), into exhalant region (CS), secondary settling tank (S2) is flowed into from exhalant region (CS) through high liquid level connecting tube (P8), it is last processed Water outlet is discharged from the outlet pipe (P3) of secondary settling tank (S2)；Pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP), in sink Area (S1) blender is opened；Aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) are in High liquid level (H) is run；Sludge surmounts pipe (P4) water (flow) direction and flows to the areas Zhong Chen (S1) by denitrification zone (ANP).

Preferably, pre- anoxic zone (PreA) residence time is 0.5-1.0h, and anaerobic zone (AP) residence time is 1.5-2.5h, the areas Zhong Chen (S1) residence time be 2.0-4.0h, aerobic decarburization area (OC) the residence time 0.5-2.0h, Exhalant region (CS) residence time≤0.5h；Aerobic nitrification area (ON) residence time nitrifies area according to aerobic nitrification area (ON) Load determines that it is 0.0004-0.0012kgN/m that aerobic nitrification area (ON), which nitrifies volume loading rate,²/d；Aerobic decarburization area (OC) stops Time determines that aerobic decarburization area (OC) organic area load is 0.004- according to aerobic decarburization area (OC) organic area load 0.012kgBOD/m²/d；Denitrification zone (ANP) residence time is according to the determination of denitrification zone (ANP) denitrification sludge loading, anti-nitre Change area (ANP) denitrification sludge loading is 0.03-0.06kgN/kgMLSS/d.

Preferably, when system by it is described surmount sludge operational mode operation when, aerobic nitrification area (ON) sludge concentration< 0.5g/L, the anaerobic zone (AP), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) sludge concentration be 3- 8g/L；The sludge age of suspended sludge is 4-12d in system；Flow of inlet water is Q, and main water inlet tube (P1) flow is 80%-90%Q, dirty Mud return duct (P5) flow is 30%-120%Q, and sludge surmounts the 85%-100% that pipe (P4) flow is mud return line (P5) flow； The DO of the aerobic nitrification area (ON) is 2.0-6.0mg/L, and the DO of the aerobic decarburization area (OC) is 1.5-4.5mg/L, described The DO of exhalant region (CS) is 1.0-3.0mg/L；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen<When 1.5mg/L, DO is reduced, every time It reduces and is no more than 15%, every time adjustment interval at least 4h；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen>When 3mg/L, DO is improved, often Secondary improve is no more than 15%, every time adjustment interval at least 4h；Total tp removal rate>90% or water outlet TP<1mg/L, Δ BOD/ Δs TN<4； The areas system Nei Ge maximum stream flow flux is no more than 2.2Q；The sludge phosphorus content of returned sludge>4%；

When system by the reflux nitrification liquid operational mode run when, the anaerobic zone (AP), denitrification zone (ANP), it is aerobic take off Carbon area (OC), exhalant region (CS) sludge concentration be 3-8g/L；The sludge age of suspended sludge is 8-15d in system；Flow of inlet water For Q, main water inlet tube (P1) flow is 80%-90%Q, and mud return line (P5) flow is 30%-120%Q, and sludge surmounts pipe (P4) stream Amount is 100%-300%Q；The DO of the aerobic nitrification area (ON) is 2.0-6.0mg/L, and the DO of the aerobic decarburization area (OC) is The DO of 1.5-4.5mg/L, the exhalant region (CS) are 1.0-3.0mg/L；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen<1.5mg/ When L, DO is reduced, reduces be no more than 15% every time, every time adjustment interval at least 4h；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen> When 3mg/L, DO is improved, improves be no more than 15% every time, every time adjustment interval at least 4h；Total tp removal rate>75% or water outlet TP< 1.5mg/L, Δ BOD/ Δs TN<5；The areas system Nei Ge maximum stream flow flux is no more than 5Q；The sludge phosphorus content of returned sludge> 2.5%。

A kind of double mode sewerage nitrogen and phosphor processing method, which is characterized in that adjust operational mode according to following steps：

1）Initial option operational mode, when intake C/N≤4 when, by surmounting sludge operational mode；As water inlet C/N>When 4, by reflux Nitrification liquid operational mode；

2）Surmount sludge operational mode and switches to reflux nitrification liquid operational mode, when system is by the operation of sludge operational mode is surmounted, When aerobic nitrification zone (ON) DO is 5.5-6.0mg/L, the water outlet aerobic nitrification area (ON) ammonia nitrogen is still>When 3mg/L, reflux is switched to Nitrification liquid operational mode；

3）Reflux nitrification liquid operational mode, which switches to, surmounts sludge operational mode, when system is by reflux nitrification liquid operational mode, when Aerobic nitrification area (ON) DO is 2.0-2.5mg/L, and the water outlet aerobic nitrification area (ON) ammonia nitrogen is still<When 1.5mg/L, switches to and surmount Sludge operational mode.

Known to people for the industry, exhalant region (CS) is mainly used for stablizing liquid level and reduces water outlet DO, to prevent dirt Mud settles, and stirring or a small amount of aeration can be arranged；Micro-pore aeration both can be used in aeration, and perforated pipe aerating regulation can also be used；It is described porous Plate, bore size are less than suspending carrier diameter, filler are prevented to be lost in, and porous plate suqare is according to mass-flux and crosses orifice meter It calculates, general via flow velocity is no more than 60m/h.

Known to people for the industry, mud return line (P5) flow is RQ, and R is return sludge ratio, and R is generally 30%-120%, R are generally selected according to sludge character, ensure sludge concentration in reactor, representative value 60%-100%.

Known to people for the industry, the selection of sludge concentration is influenced by influent quality, premised on sludge age controls, Select reasonable sludge concentration.

Known to people for the industry, the residence time of denitrification zone and pool capacity design are determined according to denitrification rate； The residence time value of each subregion can be determined present invention provide that in range according to design experiences and industry standard.

Known to people for the industry, filling rate adds the volume of suspending carrier natural packing, and adds region The ratio of pool capacity, to ensure under normal aeration condition, filler can not generate accumulation in pond, and filling rate needs≤60%；

Voidage, i.e. the voidage percentage of the total volume of unit volume suspending carrier, voidage is bigger, adds suspension and carries Influence of the body to pool capacity is smaller, when such as voidage 90%, 1m³Pool capacity, when filling rate 100%, volume is shared by suspending carrier itself 0.1m³, when filling rate 50%, volume shared by suspending carrier itself is 0.05m³；

Specific surface area, i.e., the surface area that unit suspending carrier can be provided, the ratio with the unit volume of suspending carrier natural packing Example, unit m²/m³；

Δ BOD/ Δ TN, i.e. (system water inlet BOD- systems are discharged BOD)/(system water inlet TN- systems are discharged TN), for tradition A²General Δ BOD/ Δs TN when/O techniques with denitrogenation are main>4, when good denitrification dephosphorization effect general Δ BOD/ Δs TN>7, work as Δ BOD/ΔTN<Show that system realizes TN removals with lower carbon source demand when 4；

Mass-flux, actual flow synthesis when referring to each subregion actual motion in reaction tank including water inlet and all kinds of reflux； For traditional A²/ O techniques, if flow of inlet water be Q1, return sludge ratio 100%, mixed liquid recycle ratio 300%, then anaerobic zone, lack Oxygen area, aerobic zone mass-flux be 2Q1,5Q1,5Q1 respectively, maximum stream flow flux is 5Q1；For the present invention, if feed water flow Amount is Q2, and the water inlet of pre- anoxic zone is 10%Q2, and anaerobic zone water inlet is 90%Q2, return sludge ratio 100%, and sludge surmounts pipe flow and is 100%Q2, then pre- anoxic zone, anaerobic zone, the areas Zhong Chen, aerobic nitrification area, denitrification zone, aerobic decarburization area mass-flux difference For 1.1Q2,2Q2,2Q2, Q2,2Q2,2Q2, maximum stream flow flux is 2Q2；

The sludge age of suspended sludge in system does not consider the sludge age of suspended filler biofilm part, dense according only to system sludge The sludge age for the suspended sludge that degree and sludge volume calculate；

Sludge phosphorus content, the i.e. phosphorus content of unit mass sludge, it is dirty if biological phosphor-removing effect is preferable in Biological Phosphorus Removal Processes Mud phosphorus content is generally in 3-6%；For traditional A²/ O techniques, general sludge phosphorus content is in 1.5-3.5%；

Volume loading rate, the i.e. biomembrane of per surface area are nitrified, the amount of ammonia nitrogen, kgN/m can be aoxidized daily²/d；Aerobic nitrification Area nitrifies volume loading rate, i.e. flow of inlet water × (system influent ammonia nitrogen-system is discharged ammonia nitrogen)/aerobic nitrification area suspending carrier surface The sum of product；

Organic area load, the i.e. biomembrane of per surface area, can aoxidize the amount of BOD, kgBOD/m daily²/ d, BOD are referred both to BOD₅;Aerobic decarburization area organic area load, i.e. flow of inlet water × (1+ return sludge ratios) × (aerobic decarburization area water inlet BOD- is good The sum of oxygen decarburization area is discharged BOD)/aerobic decarburization area suspending carrier surface area；

Denitrification sludge loading, i.e. unit mass sludge are capable of the amount of denitrifying nitrate, kgN/kgMLSS/d daily；Instead Nitrification zone denitrification sludge loading, i.e. flow of inlet water × (system water inlet TN- systems are discharged TN)/(denitrification zone pool capacity × anti-nitre Change area's sludge concentration);

Water inlet C/N refers to system water inlet BOD/ systems water inlet TN, general to require, biological denitrificaion requirement water inlet C/N>4, biological denitrificaion Water inlet C/N is required when dephosphorization>7, and domestic general sanitary sewage water inlet C/N is universal<4, belong to carbon source deficiency, needs outer throwing carbon Source.

Known to people for the industry, pure membrane process, that is, microorganism is mainly grown in a manner of attached state biomembrane, due to There is biomembrane aging in the process to fall off, therefore there are a small amount of suspended state microorganism, general suspended state sludge concentrations<0.5g/L；Mud The compound i.e. microorganism of film is grown in a manner of attached state biomembrane and suspended state activated sludge simultaneously, general suspended state sludge concentration> 2.0g/L。

Pre- anoxic zone inlet damper (D1) is arranged to be intended to that water inlet can be sufficiently mixed with returned sludge, quickly consumption reflux The nitrate carried secretly in sludge, while preventing short stream in pre- anoxic zone (PreA)；Setting denitrification zone inlet damper (D2) is intended to Nitrification liquid can be sufficiently mixed with the sludge surmounted, quickly consumes the molecular state dissolved oxygen carried secretly in nitrification liquid, prevents simultaneously Short stream in denitrification zone (ANP)；The setting of exhalant region (CS) is mainly used for stablizing water outlet liquid level, and reduces the dissolving of water outlet Oxygen, exhalant region (CS) are not aerated or are aerated on a small quantity using perforated pipe, be only used for stirring；To prevent returned sludge will be in water inlet VFA quickly consumes light, therefore only branch's water inlet pipe (P2) flow 10%-20%Q enters pre- anoxic zone (PreA), overwhelming majority water inlet Flow is directly entered anaerobic zone (AP)；

System provides two kinds of operational modes, and the mainly control of the areas Zhong Chen (S1), sludge surmounts flow direction and stream in pipe (P4) The mode of communicating of amount, the water level of each functional areas, reaction tank (S0) and secondary settling tank (S2)；

When system, which is in, surmounts sludge operational mode, the areas Zhong Chen (S1) utilizes bucket (ND), reinforcement sludge precipitation and concentration, carries High sludge surmounts sludge concentration in pipe (P4), reduces flow, and sludge surmounts pipe (P4) flow direction and flowed to instead by the areas Zhong Chen (S1) at this time Nitrification zone (ANP), flow 80%-100%Q, aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area in system (OC), exhalant region (CS) is in low liquid level (L), and reaction tank (S0) is connected to by low liquid level connecting tube (P7) with secondary settling tank (S2)； Between the areas Zhong Chen (S1) and aerobic nitrification zone (ON), flow is mainly used for aerobic nitrification area (ON) mass-flux by dropping to enter Control；

When system is in reflux nitrification liquid operational mode, the areas Zhong Chen (S1) turn on agitator, the areas Zhong Chen (S1) is used as denitrification Function, at this time sludge surmount pipe (P4) flow direction the areas Zhong Chen (S1) flowed to by denitrification zone (ANP), flow 100%-300%Q is Tong Nei aerobic nitrifications area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) are in high liquid level (H), reaction Pond (S0) is connected to by high liquid level connecting tube (P8) with secondary settling tank (S2)；

The pre- anoxic zone (PreA) of two kinds of operational modes, anaerobic zone (AP), the areas Zhong Chen (S1) water level all same, are in high liquid level (H)。

When system, which is in, surmounts sludge operational mode, the areas system Nei Ge maximum stream flow flux is no more than 2.2Q, predominantly Denitrification zone (ANP) provides high concentration phosphorus hydrochlorate, nitrate, organic concentration condition；The sludge age of suspended sludge is in system 4-12d, mainly control system are short sludge age, are more suitable for polyP bacteria and grow, and tradition A²The general sludge age of/O techniques is 15- 25d；The sludge phosphorus content of returned sludge>4%, show that biological phosphor-removing effect is good in system；Aerobic nitrification area (ON) sludge concentration <0.5g/L enters aerobic nitrification area (ON) for limiting suspended state sludge, and aerobic nitrification area (ON) at this time is pure membrane process；Institute The DO for stating aerobic nitrification area (ON) is 2.0-6.0mg/L, meets nitration condition, and with the increase of DO, nitrification load gradually carries Height, according to the conditions of demand of nitrification, adjusting DO in system.

When system is in reflux nitrification liquid operational mode, it is 100%-300%Q that sludge, which surmounts pipe (P4) flow, is played back Flow the effect of nitrification liquid；Total tp removal rate>75% or water outlet TP<1.5mg/L, Δ BOD/ Δs TN<5；The areas system Nei Ge maximum stream flow Flux is no more than 5Q；The sludge phosphorus content of returned sludge>2.5%.

When system designs, general anaerobic zone (AP) residence time is 1.5-2.5h, and pre- anoxic zone (PreA) residence time is The area 0.5-1.0h, Zhong Chen (S1) residence time is 1.5-3.0h, exhalant region (CS) residence time<0.5h, aerobic decarburization area (OC) Residence time 0.5-2.0h；According to nitrification volume loading rate design, it is negative that aerobic nitrification area (ON) nitrifies area in aerobic nitrification area (ON) Lotus is 0.0004-0.0012kgN/m²/ d is determined outstanding according to required suspending carrier surface area and floating stuffing effective ratio area Float carrier dosage determines pool capacity according to suspending carrier dosage and filling rate；Due to the nitrification of system occur mainly in it is aerobic Nitrification zone (ON), when calculating nitrification volume loading rate, according to flow of inlet water × (system influent ammonia nitrogen-system be discharged ammonia nitrogen)/aerobic The sum of nitrification zone suspending carrier surface area；Aerobic decarburization area (OC) is designed according to organic volumetric loading, and aerobic decarburization area (OC) has Machine volume loading rate is 0.004-0.012kgBOD/m²/ d, according to required suspending carrier surface area and the effective specific surface of floating stuffing Product determines suspending carrier dosage, determines pool capacity according to suspending carrier dosage and filling rate, when calculating organic area load, presses Shine into water flow × (1+ return sludge ratios) × (the aerobic aerobic decarburization area water outlet BOD of decarburization area water inlet BOD-)/aerobic decarburization area The sum of suspending carrier surface area, aerobic decarburization area intakes BOD generally in 15-40mg/L at this time, while to consider actual flow Flux；Denitrification zone (ANP) is designed according to denitrification sludge loading, and denitrification zone (ANP) denitrification sludge loading is 0.03- 0.06kgN/kgMLSS/d determines pool capacity according to sludge concentration；Associated loadings are by the shadow of the factors such as temperature, pH, DO, organic matter It rings；Suspending carrier filling rate is 30%-60%, and suspending carrier filling rate is excessive, can expand and add region pool capacity, reduces filling rate； Suspending carrier filling rate is too small, can reduce and add region pool capacity, increases filling rate；If system has the demand for increasing load from now on, Filling rate can remove the limit, and wait for that load increase from now on improves filling rate；If system has higher requirements for occupation of land, on filling rate is desirable Limit.

Core reasons using two kinds of operational modes are the influence being into water C/N to system.When intake C/N≤4 when, belong to In carbon source deficiency state, the sludge operational mode that surmounts based on denitrification dephosphorization is used to can get optimal processing effect at this time； But the C/N in system>When 4, because water-inlet carbon source is relatively sufficient, may have carbon source to be flowed into aerobic nitrification area (ON) influences nitrification Effect, i.e., when aerobic nitrification zone (ON) DO, which has reached, requires the upper limit, the water outlet aerobic nitrification area (ON) ammonia nitrogen is still>3mg/L, this When need strengthen aerobic nitrification area (ON) before organic matter removal effect and aerobic nitrification area (ON) nitrification ability.If At the beginning of design, to ensure water problems, using lower load values, although can get stable treatment effect, not enough pass through Ji；It is also contemplated that the influence of change of water quality in operational process simultaneously.It can by the way of pure film and the switching of mud membrane compound technology Balance investment cost and operation stability well.If system nitrification ability is insufficient, switched to from sludge operational mode is surmounted Flow back nitrification liquid operational mode, and medium sediment pool (S1) is used as denitrification function, accelerates consumption carbon source, and surmount pipe (P4) instead from sludge It largely flows back nitrification liquid to from denitrification zone (ANP) to the areas Zhong Chen (S1), accelerates organic matter consumption.At this point, aerobic nitrification area (ON) become mud membrane compound technology from pure membrane process, although the nitrification volume loading rate of aerobic nitrification area (ON) biomembrane can be reduced, But sludge age is extended, suspended sludge part is increased, overall nitrification ability is enhanced, while also because extending sludge age meeting Reduce biological phosphor-removing effect.Substantially, surmount sludge operational mode and can get best removal effect and utilization of carbon source, and flow back Nitrification liquid operational mode is then preferential to meet ammonia nitrogen removal effect, may reduce utilization of carbon source rate.

The method have the benefit that：

1）High-efficient denitrification and dephosphorization, TN removal rates>80%, TP removal rate>90%, it is far above traditional handicraft；

2）Energy saving in running, when using sludge operational mode is surmounted, maximum stream flow flux only 2.2Q in reaction tank of the present invention is remote low In traditional A²The 15-25Q of the 5Q and conventional oxidation ditch technique of/O techniques；For floating stuffing area, since DO directly affects nitre Change load, DO can be adjusted flexibly according to influent load, realizes energy-saving；

3）Low-carbon is run, water inlet C/N required when denitrogenating phosphorus can be effectively reduced；Traditional handicraft can be realized efficient de- When nitrogen dephosphorization, need to intake C/N>7, it, can be in water inlet C/N for the present invention<High-efficient denitrification and dephosphorization is completed when 4；

4）Load is high, takes up an area province, and the separation of microorganisms of nitrogen and phosphors removal system, nitrifying process is dependent on aerobic nitrification area suspending carrier Nitrifying bacteria community, denitrification process and dephosphorization process depend on suspended sludge, and suspended sludge does not enter aerobic nitrification area, realize Thorough autotrophy flora is detached with heterotrophism flora, is conducive to independent control, is created respective optimum condition for respective flora, is handled load Height reduces 20%-40% compared with traditional handicraft and takes up an area；

5）It realizes denitrification dephosphorization, creates the region of high phosphate, nitrate, organic concentration, created for denitrification dephosphorization Good condition；Traditional handicraft is bigger due to always flowing back, and denitrification zone is difficult to realize high concentration region；The present invention effectively reduces Mass-flux can realize Super matrix concentration, and anaerobic zone sludge absorption large amount of organic, be directly entered denitrification zone, improve Utilization of carbon source efficiency；

6）TN removal rates are not limited by when aerobic/non-aerobic ratio that flows back, traditional A²/ O techniques are anoxic zone by reflux type Nitrate is provided, to ensure that continuous flow plug-flow state, general total reflux ratio are no more than 400%, theoretically TN removal rates are no more than 80%；The present invention uses single flow to provide nitrate for denitrification zone, and TN removal rates are not limited by reflux ratio；Traditional A²/ O techniques Consider nitrifying bacteria community eubolism, it is desirable that aerobic HRT>Non- aerobic HRT, due to realizing flora separation, system is no longer by secondary limit System；

7）Control is simple, is easy to operational management conveniently, compares driving by double-energy, single-stage Biosystems control is simple；Compared to fixed Filler, operational management is convenient, and the update of dynamic biological film, the anxiety without dead mud or blocking are realized by suspending carrier fluid mapper process；

8）Flexible operation, for water inlet C/N difference and system nitrification ability, flexible arrangement operational mode.

Description of the drawings

Fig. 1 is the flow sheet of the present invention.

In figure：S0 is reaction tank, and S2 is secondary settling tank, and PreA is pre- anoxic zone, and AP is anaerobic zone, and S1 is the areas Zhong Chen, and ON is Aerobic nitrification area, ANP are denitrification zone, and OC is aerobic decarburization area, and CS is exhalant region, and P1 is main water inlet tube, and P2 is intake for branch Pipe, P3 are outlet pipe, and P4 is that sludge surmounts pipe, and P5 is mud return line, and P6 is excess sludge delivery pipe, and P7 connects for low liquid level Pipe, P8 are high liquid level connecting tube, and G1 is pre- anoxic zone anaerobic zone partition wall, and G2 is to sink to separate wall in anaerobic zone, and G3 is that the areas Zhong Chen are good Oxygen nitrification zone partition wall, G4 are aerobic nitrification zone denitrification zone partition wall, and G5 is that the aerobic decarburization in denitrification zone separates wall, and G6 is aerobic de- Carbon area exhalant region partition wall, K1 are pre- anoxic zone anaerobic zone hole, and K2 is the anaerobic zone areas Zhong Chen hole, and K3 is the areas Zhong Chen aerobic nitrification Area's hole, K4 are aerobic nitrification zone denitrification zone hole, and K5 is the aerobic decarburization area hole in denitrification zone, and K6 is that aerobic decarburization area goes out Pool hole, W1 are aerobic nitrification zone denitrification zone porous plate, and W2 is aerobic decarburization area exhalant region porous plate, and D1 is pre- anoxic zone Inlet damper, D2 are denitrification zone inlet damper, and ND is bucket, and J1 is pre- anoxic zone blender, and J2 is anaerobic zone blender, J3 For denitrification zone blender, J4 is the areas Zhong Chen blender, and H is high liquid level, and L is low liquid level.

Specific implementation mode

In order to make the purpose of the present invention, technical solution and advantage become apparent from, it is clear, below with reference to specific embodiment, The present invention is described in more detail.

A kind of double mode sewerage nitrogen and phosphor processing system of present invention offer and method, can solve traditional denitrification dephosphorization technique efficiency The problems such as low, outer throwing carbon source amount height, the big increase energy consumption of reflux ratio, denitrogenation dephosphorizing are difficult to take into account, removes suitable for bio-denitrifying sewage Phosphorus and sewage treatment plant's upgrading.

The following examples are used to illustrate the present invention, but are not intended to limit the scope of the present invention..The present invention, in conjunction with shown in Fig. 1, System is made of reaction tank (S0), secondary settling tank (S2) and connecting line；Reaction tank (S0) is followed successively by pre- from water inlet end to water outlet Anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1), aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS)；The pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP), the areas Zhong Chen (S1) are equipped with Blender；The areas Zhong Chen (S1) bottom is equipped with bucket (ND), and the areas Zhong Chen (S1) bottom slope aspect bucket (ND), the gradient is in 1%-3%； The aerobic nitrification area (ON), aerobic decarburization area (OC) are equipped with aeration；The aerobic nitrification area (ON) and aerobic decarburization area (OC) suspending carrier is added；The suspending vehicle density is 0.90-0.98g/cm³, voidage>85%, filling rate is in 10%- 60%, specific surface area >=300m²/m³；

The pre- anoxic zone that the pre- anoxic zone (PreA) and anaerobic zone (AP) are equipped with by pre- anoxic zone anaerobic zone partition wall (G1) Anaerobic zone hole (K1) communicates；The anaerobic zone (AP) and the areas Zhong Chen (S1) separate what wall (G2) was equipped with by sinking in anaerobic zone The anaerobic zone areas Zhong Chen hole (K2) communicates；The areas Zhong Chen (S1) and aerobic nitrification zone (ON) are separated by the areas Zhong Chen aerobic nitrification Aerobic nitrification area of the areas the Zhong Chen hole (K3) that wall (G3) is equipped with communicates；The aerobic nitrification area (ON) and denitrification zone (ANP) Aerobic nitrification area denitrification zone hole (K4) being equipped with by aerobic nitrification area denitrification zone partition wall (G4) communicates；It is described aerobic Nitrification zone denitrification zone hole (K4) is equipped with aerobic nitrification area denitrification zone porous plate (W1)；The denitrification zone (ANP) and Aerobic decarburization area (OC) separates the aerobic decarburization area hole in denitrification zone that wall (G5) is equipped with by the aerobic decarburization in denitrification zone (K5) it communicates；It is good that the aerobic decarburization area (OC) and exhalant region (CS) are equipped with by aerobic decarburization area exhalant region partition wall (G6) Oxygen decarburization area exhalant region hole (K6) communicates；The aerobic decarburization area exhalant region hole (K6) is equipped with aerobic decarburization area exhalant region Porous plate (W2)；

The connecting line includes that main water inlet tube (P1), branch's water inlet pipe (P2), outlet pipe (P3), sludge surmount pipe (P4), mud return line (P5), excess sludge delivery pipe (P6), low liquid level connecting tube (P7), high liquid level connecting tube (P8)；It is described Main water inlet tube (P1) is communicated with anaerobic zone (AP) front bottom end；Before described branch's water inlet pipe one end (P2) and pre- anoxic zone (PreA) End middle part communicates, and the other end is communicated with main water inlet tube (P1)；The sludge surmounts pipe one end (P4) and the bottom the areas Zhong Chen (S1) Bucket (ND) communicates, and the other end is communicated with the front bottom end of denitrification zone (ANP)；Described mud return line one end (P5) is heavy with two The bottom pond (S2) communicates, and the other end is communicated with pre- anoxic zone (PreA) front center；The excess sludge delivery pipe (P6) and two Heavy bottom pond (S2) communicates；Exhalant region (CS) passes through low liquid level connecting tube (P7), high liquid level connecting tube respectively with secondary settling tank (S2) (P8) it communicates；It is communicated at the top of the outlet pipe (P3) and secondary settling tank (S2)；Sludge surmounts pipe (P4) and mud return line (P5) point It She You not sludge pump；The low liquid level connecting tube center (P7) is identical as low liquid level (L) absolute altitude；The high liquid level connecting tube center (P8) and height Liquid level (H) absolute altitude is identical.

Pre- anoxic zone (PreA) front end is equipped with pre- anoxic zone inlet damper (D1), pre- anoxic zone inlet damper (D1) top End is in the above 0.5m-1.0m of anaerobic zone (AP) water surface, and the pre- anoxic zone inlet damper bottom end (D1) is more than anaerobic zone (AP) bottom of pond 0.5m-1.0m；Denitrification zone (ANP) front end is equipped with denitrification zone inlet damper (D2), denitrification zone inlet damper (D2) Top is in denitrification zone (ANP) high liquid level (H) the above 0.5m-1.0m of the water surface, and the inlet damper bottom end (D2) in denitrification zone is in anti-nitre Change the above 0.5m-1.0m of area (ANP) bottom of pond.

The pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1) water surface absolute altitude are identical, with high liquid level (H) absolute altitude It is identical；The aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) water surface absolute altitude are identical, There are two high liquid level (H), low liquid level (L) water surface absolute altitudes；High liquid level (H) absolute altitude is bigger 0.2-0.4m than low liquid level (L) absolute altitude.

Described to surmount sludge operational mode, a water inlet part enters pre- anoxic zone (PreA) by branch's water inlet pipe (P2), A part is directly entered anaerobic zone (AP) by main water inlet tube (P1)；Mud return line (P5) is by returned sludge from secondary settling tank (S2) Pre- anoxic zone (PreA) is passed back into, and is quickly mixed before pre- anoxic zone inlet damper (D1) with the water inlet of branch's water inlet pipe (P2) It closes；Mud mixture in pre- anoxic zone (PreA) enters anaerobic zone (AP) by pre- anoxic zone anaerobic zone hole (K1)；Anaerobism Area (AP) interior mud mixture enters the areas Zhong Chen (S1) by the anaerobic zone areas Zhong Chen hole (K2), and after precipitation, supernatant is logical Aerobic nitrification area of the areas Guo Zhongchen hole (K3) drop enters aerobic nitrification area (ON), and the sludge of sedimentation passes through after entering bucket (ND) Sludge surmounts pipe (P4) and is directly entered denitrification zone (ANP) front bottom end；Water in aerobic nitrification area (ON) passes through aerobic nitrification The aerobic nitrification area denitrification zone porous plate (W1) that area denitrification zone hole (K4) is equipped with enters the front end denitrification zone (ANP), And before the denitrification zone inlet damper (D2) with the sludge that pipe (P4) surmounts surmounted by sludge mix；Denitrification zone (ANP) Mud mixture enters aerobic decarburization area (OC) by the aerobic decarburization area hole (K5) in denitrification zone；The mud of aerobic decarburization area (OC) The aerobic decarburization area exhalant region porous plate (W2) that aqueous mixtures are equipped with by aerobic decarburization area exhalant region hole (K6), into going out Pool (CS) flows into secondary settling tank (S2) from exhalant region (CS) through low liquid level connecting tube (P7), and last processed water outlet is heavy from two The outlet pipe (P3) in pond (S2) discharges；Pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP) blender are opened；It is good Oxygen nitrification zone (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) are in low liquid level (L) operation；Sludge is super More pipe (P4) water (flow) direction flows to denitrification zone (ANP) by the areas Zhong Chen (S1)；

Embodiment 1：

Discharge of sewage Q is 100000m³/ d, be sanitary sewage, water inlet mean value be ammonia nitrogen 45mg/L, TN55mg/L, TP6mg/L, BOD160mg/L, Effluent criteria are ammonia nitrogen<3mg/L、TN<10mg/L、TP<0.5mg/L、BOD<10mg/L, water inlet BOD/TN= 2.91, using device as described in Figure 1.

Pre- anoxic zone (PreA) residence time is 0.5h, and anaerobic zone (AP) residence time is 2.0h, and the areas Zhong Chen (S1) is stopped Time is 2.5h, exhalant region (CS) residence time 0.5h；Aerobic nitrification area (ON) residence time is 2.5h, using specific surface area 800m²/m³Suspending carrier, filling rate 50%；Aerobic decarburization area (OC) residence time is 0.5h, using specific surface area 800m²/m³It is outstanding Float carrier, filling rate 30%；Denitrification zone (ANP) residence time is 4.5h；Total residence time 13.0h.

System, which uses, surmounts sludge operational mode, aerobic nitrification area (ON) sludge concentration 0.3g/L, anaerobic zone (AP), anti-nitre Change area (ANP), aerobic decarburization area (OC), exhalant region (CS) sludge concentration be 4-4.5g/L, the sludge of suspended sludge in system Age is 6-8d.Main water inlet tube (P1) flow is 80%-90%Q, and mud return line (P5) flow is 70%-90%Q, and sludge surmounts pipe (P4) flow is 70%-90%Q；The DO in aerobic nitrification area (ON) is 2.0-6.0mg/L, and the DO of aerobic decarburization area (OC) is 1.5- The DO of 4.5mg/L, exhalant region (CS) are 1.0-3.0mg/L.

The areas system Nei Ge maximum stream flow flux is 1.9Q；The sludge phosphorus content 4.8% of returned sludge.

Water outlet TN mean values be 8.2mg/L, water outlet TP mean values be 0.4mg/L, water outlet BOD mean values be 6mg/L, TP removal rates= Δ TP/ water inlets TP=(6-0.4)/6=93.3%, Δ BOD/ Δs TN=(160-6)/(55-8.2)=3.29.

Embodiment 2：

The operation of embodiment 1 meets with influent quality impact to 300d, and larger change occurs for influent quality, and water inlet BOD reaches 200mg/ L, the variation of other index averages is little, and aerobic nitrification area (ON) DO is 5.5-6.0mg/L, the water outlet aerobic nitrification area (ON) at this time Ammonia nitrogen be 4.5mg/L still>3mg/L, total ammonia nitrogen that is discharged is by before<1mg/L is improved to 3.5mg/L, switches to reflux nitrification liquid Operational mode；

When the nitrification liquid operational mode that flows back, the sludge age of suspended sludge increases to as 12-15d in system；Flow of inlet water is Q, it is main into Water pipe (P1) flow is 80%-90%Q, and mud return line (P5) flow is 70%-90%Q, and it is 200% that sludge, which surmounts pipe (P4) flow, Q；The DO in aerobic nitrification area (ON) is 4.0-6.0mg/L, and the DO of aerobic decarburization area (OC) is 1.5-4.5mg/L, exhalant region (CS) DO be 1.0-3.0mg/L；System stably reaching standard, the water outlet aerobic nitrification area (ON) ammonia nitrogen are gradually down to 3mg/L hereinafter, always going out Water ammonia nitrogen is down to 1mg/L or less；After running 30d, system influent quality restores normal, ensures aerobic nitrification under the premise for the treatment of effect The DO in area (ON) is gradually reduced to 2.0-2.5mg/L, switches to and surmounts sludge operational mode.

Water outlet TN mean values are 9.6mg/L, and water outlet TP mean values are 1.36mg/L, and water outlet BOD mean values are 10mg/L, TP removal rates The TP/ water inlets of=Δ TP=(6-1.36)/6=77.3%, Δ BOD/ Δs TN=(200-10)/(55-9.6)=4.18.

When surmounting sludge operational mode, aerobic nitrification area (ON) sludge concentration 0.3g/L, anaerobic zone (AP), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) sludge concentration be 4-4.5g/L, the sludge age of suspended sludge is in system 6-8d.Main water inlet tube (P1) flow is 80%-90%Q, and mud return line (P5) flow is 70%-90%Q, and sludge surmounts pipe (P4) stream Amount is 70%-90%Q；The DO in aerobic nitrification area (ON) is 2.0-6.0mg/L, and the DO of aerobic decarburization area (OC) is 1.5-4.5mg/L, The DO of exhalant region (CS) is 1.0-3.0mg/L.

Water outlet TN mean values be 8.1mg/L, water outlet TP mean values be 0.31mg/L, water outlet BOD mean values be 5mg/L, TP removal rates= Δ TP/ water inlets TP=(6-0.31)/6=94.8%, Δ BOD/ Δs TN=(160-5)/(55-8.1)=3.30.

Although more herein used denitrification zone, mud return line, sludge to surmount the terms such as pipe, not It rules out the possibility of using other terms, those skilled in the art simply replace to what these terms were done under the inspiration of the present invention It changes, it should all be within protection scope of the present invention.Prior art is taken or used for reference in the part that do not addressed in aforesaid way can be real It is existing.The above is only a preferred embodiment of the present invention, it is not intended to restrict the invention, it is noted that this technology is led For the those of ordinary skill in domain, without departing from the technical principles of the invention, several improvements and modifications can also be made, These improvements and modifications also should be regarded as protection scope of the present invention.

Claims

1. a kind of double mode sewerage nitrogen and phosphor processing system, which is characterized in that system is by reaction tank (S0), secondary settling tank (S2) and connection Pipeline forms；Reaction tank (S0) is followed successively by pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen from water inlet end to water outlet (S1), aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS).

2. a kind of double mode sewerage nitrogen and phosphor processing system according to claim 1, which is characterized in that the pre- anoxic zone (PreA), anaerobic zone (AP), denitrification zone (ANP), the areas Zhong Chen (S1) are equipped with blender；The areas Zhong Chen (S1) bottom is equipped with Bucket (ND), the areas Zhong Chen (S1) bottom slope aspect bucket (ND), the gradient is in 1%-3%；The aerobic nitrification area (ON), aerobic decarburization area (OC) it is equipped with aeration；The aerobic nitrification area (ON) and aerobic decarburization area (OC) add suspending carrier；The suspending carrier Density is 0.90-0.98g/cm³, voidage>85%, filling rate is in 10%-60%, specific surface area >=300m²/m³。

3. a kind of double mode sewerage nitrogen and phosphor processing system according to claim 1, which is characterized in that the pre- anoxic zone (PreA) and anaerobic zone (AP) pre- anoxic zone anaerobic zone hole (K1) phase for being equipped with by pre- anoxic zone anaerobic zone partition wall (G1) It is logical；The anaerobic zone (AP) and the areas Zhong Chen (S1) pass through the heavy anaerobic zone areas the Zhong Chen hole for separating wall (G2) and being equipped in anaerobic zone (K2) it communicates；The areas Zhong Chen (S1) and aerobic nitrification zone (ON) are separated by the areas Zhong Chen aerobic nitrification during wall (G3) is equipped with Heavy area's aerobic nitrification area hole (K3) communicates；The aerobic nitrification area (ON) and denitrification zone (ANP) are anti-by aerobic nitrification area Aerobic nitrification area denitrification zone hole (K4) that nitrification zone partition wall (G4) is equipped with communicates；Aerobic nitrification area denitrification zone hole Hole (K4) is equipped with aerobic nitrification area denitrification zone porous plate (W1)；The denitrification zone (ANP) and aerobic decarburization area (OC) are logical It crosses the aerobic decarburization in denitrification zone and separates the aerobic decarburization area hole (K5) in denitrification zone that wall (G5) is equipped with and communicate；It is described aerobic de- The aerobic decarburization area exhalant region hole that carbon area (OC) and exhalant region (CS) are equipped with by aerobic decarburization area exhalant region partition wall (G6) (K6) it communicates；The aerobic decarburization area exhalant region hole (K6) is equipped with aerobic decarburization area exhalant region porous plate (W2)；

4. a kind of double mode sewerage nitrogen and phosphor processing system according to claim 1, which is characterized in that the connecting line packet It includes main water inlet tube (P1), branch's water inlet pipe (P2), outlet pipe (P3), sludge and surmounts pipe (P4), mud return line (P5), remaining dirt Mud delivery pipe (P6), low liquid level connecting tube (P7), high liquid level connecting tube (P8)；Before the main water inlet tube (P1) and anaerobic zone (AP) End bottom communicates；Described branch's water inlet pipe one end (P2) is communicated with pre- anoxic zone (PreA) front center, the other end and main water inlet Pipe (P1) communicates；The sludge surmounts pipe one end (P4) and is communicated with the bucket (ND) of the bottom the areas Zhong Chen (S1), the other end and anti-nitre The front bottom end for changing area (ANP) communicates；Described mud return line one end (P5) is communicated with the bottom secondary settling tank (S2), the other end with it is pre- Anoxic zone (PreA) front center communicates；The excess sludge delivery pipe (P6) communicates with the bottom secondary settling tank (S2)；Exhalant region (CS) it is communicated respectively by low liquid level connecting tube (P7), high liquid level connecting tube (P8) with secondary settling tank (S2)；The outlet pipe (P3) It is communicated with secondary settling tank (S2) top；Sludge surmounts pipe (P4) and mud return line (P5) is respectively equipped with sludge pump；Low liquid level connects The center (P7) of pipe is identical as low liquid level (L) absolute altitude；The high liquid level connecting tube center (P8) is identical as high liquid level (H) absolute altitude.

5. a kind of double mode sewerage nitrogen and phosphor processing system according to claim 1, which is characterized in that the pre- anoxic zone (PreA) front end be equipped with pre- anoxic zone inlet damper (D1), the pre- anoxic zone inlet damper top (D1) anaerobic zone (AP) water surface with Upper 0.5m-1.0m, the pre- anoxic zone inlet damper bottom end (D1) is in the above 0.5m-1.0m of anaerobic zone (AP) bottom of pond；The denitrification The front end area (ANP) is equipped with denitrification zone inlet damper (D2), and the inlet damper top (D2) in denitrification zone is in denitrification zone (ANP) height Liquid level (H) above 0.5m-1.0m of the water surface, the inlet damper bottom end (D2) in denitrification zone is in the above 0.5m- of denitrification zone (ANP) bottom of pond 1.0m。

6. a kind of double mode sewerage nitrogen and phosphor processing system according to claim 1, which is characterized in that the pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1) water surface absolute altitude are identical, identical as high liquid level (H) absolute altitude；The aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) water surface absolute altitude are identical, there is high liquid level (H), low liquid level (L) two water surface absolute altitudes；High liquid level (H) absolute altitude is bigger 0.2-0.4m than low liquid level (L) absolute altitude.

7. a kind of double mode sewerage nitrogen and phosphor processing method, special using the equipment as described in claim 1-6 any claims Sign is that water inlet passes sequentially through reaction tank (S0), the secondary settling tank (S2) of system, realizes the removal of pollutant；The system comprises Surmount sludge operational mode and reflux nitrification liquid operational mode；

8. a kind of double mode sewerage nitrogen and phosphor processing method according to claim 7, which is characterized in that the pre- anoxic zone (PreA) residence time is 0.5-1.0h, and anaerobic zone (AP) residence time is 1.5-2.5h, and the areas Zhong Chen (S1) stop Time is 2.0-4.0h, aerobic decarburization area (OC) the residence time 0.5-2.0h, exhalant region (CS) residence time≤ 0.5h；Aerobic nitrification area (ON) residence time nitrifies volume loading rate according to aerobic nitrification area (ON) and determines, aerobic nitrification area (ON) Nitrification volume loading rate is 0.0004-0.0012kgN/m²/d；Aerobic decarburization area (OC) residence time is according to aerobic decarburization area (OC) Organic area load determines that aerobic decarburization area (OC) organic area load is 0.004-0.012kgBOD/m²/d；Denitrification zone (ANP) residence time determines according to denitrification zone (ANP) denitrification sludge loading, denitrification zone (ANP) denitrification sludge loading For 0.03-0.06kgN/kgMLSS/d.

9. a kind of double mode sewerage nitrogen and phosphor processing method according to claim 7, which is characterized in that when system is by described super When more sludge operational mode is run, aerobic nitrification area (ON) sludge concentration<0.5g/L, the anaerobic zone (AP), denitrification Area (ANP), aerobic decarburization area (OC), exhalant region (CS) sludge concentration be 3-8g/L；The sludge age of suspended sludge is in system 4-12d；Flow of inlet water is Q, and main water inlet tube (P1) flow is 80%-90%Q, and mud return line (P5) flow is 30%-120%Q, dirty Mud surmounts the 85%-100% that pipe (P4) flow is mud return line (P5) flow；The DO of the aerobic nitrification area (ON) is 2.0- The DO of 6.0mg/L, the aerobic decarburization area (OC) are 1.5-4.5mg/L, and the DO of the exhalant region (CS) is 1.0-3.0mg/L； When the water outlet aerobic nitrification zone (ON) ammonia nitrogen<When 1.5mg/L, DO is reduced, reduces be no more than 15% every time, each adjustment interval is extremely Few 4h；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen>When 3mg/L, DO is improved, improves be no more than 15% every time, every time adjustment interval At least 4h；Total tp removal rate>90% or water outlet TP<1mg/L, Δ BOD/ Δs TN<4；The areas system Nei Ge maximum stream flow flux is no more than 2.2Q；The sludge phosphorus content of returned sludge>4%；

10. a kind of double mode sewerage nitrogen and phosphor processing method according to claim 7, which is characterized in that according to following steps Adjust operational mode：