CN108706730A - A kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method - Google Patents
A kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method Download PDFInfo
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- CN108706730A CN108706730A CN201810555256.7A CN201810555256A CN108706730A CN 108706730 A CN108706730 A CN 108706730A CN 201810555256 A CN201810555256 A CN 201810555256A CN 108706730 A CN108706730 A CN 108706730A
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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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- 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
- C02F2101/16—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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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 present invention discloses a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method, belongs to sewage treatment field.Sewage of the present invention passes sequentially through reaction tank, secondary settling tank, realizes intensified denitrification and dephosphorization, TP Qu Chushuais >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
Technical field
The invention belongs to technical field of sewage, and in particular to a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal 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 NOX -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 NOx -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
Water inlet C/N Pu Bians <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 NOX -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 NOX -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.
Invention content
Based on above-mentioned technical problem, the present invention provides a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method.
The adopted technical solution is that：
A kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method, which is characterized in that water inlet passes sequentially through reaction tank (S0), secondary settling tank
(S2), the removal of pollutant is realized；The reaction tank (S0) is followed successively by pre- anoxic zone (PreA), anaerobism from water inlet end to water outlet
Area (AP), the areas Zhong Chen (S1), aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS).
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 1.5-3.0h, aerobic decarburization area (OC) the residence time 0.5-2.0h,
Exhalant region (CS) residence time≤0.5h.
Preferably, it is 0.0005-0.0015kgN/m that aerobic nitrification area (ON), which nitrifies volume loading rate,2/ d, aerobic decarburization area
(OC) organic area load is 0.004-0.012kgBOD/m2/ d, denitrification zone (ANP) denitrification sludge loading are 0.03-
0.06kgN/kgMLSS/d。
Preferably, aerobic nitrification area (ON) the Wu Ninongdu <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- in system
12d。
Preferably, flow of inlet water Q, main water inlet tube (P1) flow are 80%-90%Q, and mud return line (P5) flow is
30%-120%Q, sludge surmount the 85%-100% that pipe (P4) flow is mud return line (P5) flow.
Preferably, 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.
Preferably, 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,
Adjustment interval at least 4h every time；When the water outlet aerobic nitrification zone (ON) ammonia nitrogen;When 3mg/L, DO is improved, improves be no more than every time
15%, adjustment every time is spaced at least 4h.
Preferably, TP Qu Chushuais >90% or water outlet TP<1mg/L, Δ BOD/ Δs TN<4；The areas system Nei Ge maximum stream flow flux
No more than 2.2Q；The sludge Han Linshuai > of returned sludge;4%.
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 Pu Bians <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 Wu Ninongdu <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 Wu Ninongdu >
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；The areas Zhong Chen (S1) and aerobic nitrification zone (ON)
Between, flow enters the control for being mainly used for aerobic nitrification area (ON) mass-flux by dropping；To prevent returned sludge will be into
VFA in water quickly consumes light, therefore only branch's water inlet pipe (P2) flow 10%-20%Q enters pre- anoxic zone (PreA), absolutely mostly
Number flow of inlet water is directly entered anaerobic zone (AP)；Bucket, and bottom slope aspect bucket is arranged in the bottom the areas Zhong Chen (S1), predominantly strengthens
Sludge settling and concentration improve sludge and surmount sludge concentration in pipe (P4)；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 dirt of suspended sludge in system
Sludge age is 4-12d, and mainly control system is short sludge age, is more suitable for polyP bacteria and grows, and tradition A2The general sludge age of/O techniques
For 15-25d；The sludge Han Linshuai > of returned sludge;4%, show that biological phosphor-removing effect is good in system；The aerobic nitrification area
(ON) Wu Ninongdu <0.5g/L enters aerobic nitrification area (ON) for limiting suspended state sludge；The aerobic nitrification area (ON)
DO is 2.0-6.0mg/L, meets nitration condition, and with the increase of DO, and nitrification load steps up, according in system to nitrification
Conditions of demand, adjust DO.
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 0.0005-0.0015kgN/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.
The method have the benefit that：
1）High-efficient denitrification and dephosphorization, TN Qu Chushuais >80%, TP Qu Chushuai >90%, it is far above traditional handicraft；
2）Energy saving in running, maximum stream flow flux only 2.2Q in reaction tank of the present invention are far below tradition A2The 5Q and tradition of/O techniques
The 15-25Q of oxidation ditch process；It can be flexible according to influent load since DO directly affects nitrification load for floating stuffing area
DO is adjusted, is realized 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.
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 is connecting tube, G1
For pre- anoxic zone anaerobic zone partition wall, G2 is to sink to separate wall in anaerobic zone, and G3 is that the areas Zhong Chen aerobic nitrification separates wall, and G4 is aerobic nitre
The denitrification zones Hua Qu partition wall, G5 are that the aerobic decarburization in denitrification zone separates wall, and G6 is aerobic decarburization area exhalant region partition wall, and K1 is pre- lacks
Oxygen area anaerobic zone hole, K2 are the anaerobic zone areas Zhong Chen hole, and K3 is aerobic nitrification area of the areas Zhong Chen hole, and K4 is that aerobic nitrification zone is anti-
Nitrification zone hole, K5 are the aerobic decarburization area hole in denitrification zone, and K6 is aerobic decarburization area exhalant region hole, and W1 is aerobic nitrification zone
Denitrification zone porous plate, W2 be aerobic decarburization area exhalant region porous plate, D1 be pre- anoxic zone inlet damper, D2 be denitrification zone into
Water baffle, ND are bucket, and J1 is pre- anoxic zone blender, and J2 is anaerobic zone blender, and J3 is denitrification zone blender.
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.
The present invention provides a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method, can solve traditional denitrification dephosphorization technique efficiency it is low,
The problems such as outer throwing carbon source amount height, the big increase energy consumption of reflux ratio, denitrogenation dephosphorizing are difficult to take into account, be suitable for bio-denitrifying sewage dephosphorization 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) are equipped with blender；It is described
The bottom the areas Zhong Chen (S1) is equipped with bucket (ND), and the areas Zhong Chen (S1) bottom slope aspect bucket (ND), the gradient is in 1%-3%；The aerobic nitre
Change area (ON), aerobic decarburization area (OC) is equipped with aeration；The aerobic nitrification area (ON) and aerobic decarburization area (OC) add outstanding
Float carrier；The suspending vehicle density is 0.90-0.98g/cm3, Kong Xishuai >85%, filling rate in 30%-60%, specific surface area >=
300m2/m3；The pre- anoxic zone (PreA) and anaerobic zone (AP) are equipped with pre- scarce by pre- anoxic zone anaerobic zone partition wall (G1)
Oxygen area anaerobic zone hole (K1) communicates；The anaerobic zone (AP) and the areas Zhong Chen (S1) are set by sinking to separate in anaerobic zone on wall (G2)
The areas some anaerobic zone Zhong Chen hole (K2) communicates；The areas Zhong Chen (S1) and aerobic nitrification zone (ON) pass through the areas Zhong Chen aerobic nitrification
Aerobic nitrification area of the areas the Zhong Chen hole (K3) that wall (G3) is equipped with is separated to communicate；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；Institute
It states aerobic nitrification area denitrification zone hole (K4) and 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 in denitrification zone that wall (G5) is equipped with by the aerobic decarburization in denitrification zone
Hole (K5) communicates；The aerobic decarburization area (OC) and exhalant region (CS) are equipped with by aerobic decarburization area exhalant region partition wall (G6)
Aerobic decarburization area exhalant region hole (K6) communicate；The aerobic decarburization area exhalant region hole (K6) goes out equipped with aerobic decarburization area
Pool 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 centre-to-centre spacing bottom of pond distance of the areas anaerobic zone Zhong Chen hole (K2) is the 50-60% of anaerobic zone (AP) available depth；It sinks in described
The lower edge of aerobic nitrification area of area hole (K3) is identical as anaerobic zone (AP) available depth away from bottom of pond distance；The aerobic nitrification area is anti-
The upper edge of nitrification zone hole (K4) 0.5m-1.5m below denitrification zone (ANP) water surface；The aerobic decarburization area in denitrification zone hole
The upper edge in hole (K5) 0.5m-1.5m below denitrification zone (ANP) water surface；The aerobic decarburization area exhalant region hole (K6) it is upper
Along the 0.5m-1.5m below denitrification zone (ANP) water surface；The connecting line includes 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), connecting tube (P7)；
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) is communicated with secondary settling tank (S2) by connecting tube (P7)；The water outlet
It is communicated at the top of pipe (P3) and secondary settling tank (S2)；Sludge surmounts pipe (P4) and mud return line (P5) is respectively equipped with sludge pump；It is described
Pre- anoxic zone (PreA) front end is equipped with pre- anoxic zone inlet damper (D1), and pre- anoxic zone inlet damper (D1) top is in anaerobic zone
(AP) the above 0.5m-1.0m of the water surface, the pre- anoxic zone inlet damper bottom end (D1) is in the above 0.5m-1.0m of anaerobic zone (AP) bottom of pond；
Denitrification zone (ANP) front end is equipped with denitrification zone inlet damper (D2), and the inlet damper top (D2) in denitrification zone is in anti-nitre
Change area (ANP) above 0.5m-1.0m of the water surface, the inlet damper bottom end (D2) in denitrification zone is more than denitrification zone (ANP) bottom of pond
0.5m-1.0m；The pre- anoxic zone (PreA), anaerobic zone (AP), the areas Zhong Chen (S1) water surface absolute altitude are identical；The aerobic nitrification area
(ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS) water surface absolute altitude are identical；Anaerobic zone (AP) water surface absolute altitude ratio
The big 0.1-0.3m of denitrification zone (ANP) water surface absolute altitude.
A water inlet part enters pre- anoxic zone (PreA) by branch's water inlet pipe (P2), and a part passes through main water inlet tube (P1)
It is directly entered anaerobic zone (AP)；Returned sludge is passed back into pre- anoxic zone (PreA) by mud return line (P5) from secondary settling tank (S2),
And it is quickly mixed before pre- anoxic zone inlet damper (D1) with the water inlet of branch's water inlet pipe (P2)；Mud in pre- anoxic zone (PreA)
Aqueous mixtures enter anaerobic zone (AP) by pre- anoxic zone anaerobic zone hole (K1)；Anaerobic zone (AP) interior mud mixture is by detesting
The areas Zhong Chen of oxygen area hole (K2) enters the areas Zhong Chen (S1), after precipitation, realizes that mud-water separation, supernatant are aerobic by the areas Zhong Chen
Nitrification zone hole (K3) drop enters aerobic nitrification area (ON), and the sludge of sedimentation enters after bucket (ND) surmounts pipe by sludge
(P4) it is directly entered denitrification zone (ANP) front bottom end；Water in aerobic nitrification area (ON) passes through aerobic nitrification area denitrification zone
The aerobic nitrification area denitrification zone porous plate (W1) that hole (K4) is equipped with enters the front end denitrification zone (ANP), and in denitrification
Before area's inlet damper (D2) with the sludge that pipe (P4) surmounts surmounted by sludge mix；The mud mixture of denitrification zone (ANP)
Enter aerobic decarburization area (OC) by the aerobic decarburization area hole (K5) in denitrification zone；The mud mixture of aerobic decarburization area (OC) is logical
The aerobic decarburization area exhalant region porous plate (W2) that aerobic decarburization area exhalant region hole (K6) is equipped with is crossed, into exhalant region (CS),
Secondary settling tank (S2), outlet pipe of the last processed water outlet from secondary settling tank (S2) are flowed into from exhalant region (CS) through connecting tube (P7)
(P3) it discharges.
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 An Dan <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.
Aerobic nitrification area (ON) sludge concentration 0.3g/L, anaerobic zone (AP), denitrification zone (ANP), aerobic decarburization area (OC),
The sludge concentration of exhalant region (CS) is 4-4.5g/L, and the sludge age of suspended sludge is 6-8d in system.Main water inlet tube (P1) flow
For 80%-90%Q, mud return line (P5) flow is 70%-90%Q, and it is 70%-90%Q that sludge, which surmounts pipe (P4) flow,；Aerobic nitrification
The DO in area (ON) is 2.0-6.0mg/L, and the DO of aerobic decarburization area (OC) is 1.5-4.5mg/L, and the DO of exhalant region (CS) is 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=
(6-0.4)/6=93.3%>90%, Δ BOD/ Δs TN=(160-6)/(55-8.2)=3.29.
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 (8)
1. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method, which is characterized in that water inlet passes sequentially through reaction tank (S0), secondary settling tank
(S2), the removal of pollutant is realized；The reaction tank (S0) is followed successively by pre- anoxic zone (PreA), anaerobism from water inlet end to water outlet
Area (AP), the areas Zhong Chen (S1), aerobic nitrification area (ON), denitrification zone (ANP), aerobic decarburization area (OC), exhalant region (CS).
2. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, 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 1.5-3.0h, aerobic decarburization area (OC) the residence time 0.5-2.0h, exhalant region (CS) residence time≤
0.5h。
3. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that 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
0.0005-0.0015kgN/m2/d；Aerobic decarburization area (OC) residence time is true according to aerobic decarburization area (OC) organic area load
Fixed, aerobic decarburization area (OC) organic area load is 0.004-0.012kgBOD/m2/d；Denitrification zone (ANP) residence time root
It is determined according to denitrification zone (ANP) denitrification sludge loading, denitrification zone (ANP) denitrification sludge loading is 0.03-0.06kgN/
kgMLSS/d。
4. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that the aerobic nitrification
Area (ON) Wu Ninongdu <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.
5. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that flow of inlet water 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) flow and is
The 85%-100% of mud return line (P5) flow.
6. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that the aerobic nitrification
The DO in area (ON) is 2.0-6.0mg/L, and the DO of the aerobic decarburization area (OC) is 1.5-4.5mg/L, the exhalant region (CS)
DO is 1.0-3.0mg/L.
7. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that when aerobic nitrification zone
(ON) water outlet An Dan <When 1.5mg/L, DO is reduced, reduces be no more than 15% every time, every time adjustment interval at least 4h；When aerobic nitre
Change area (ON) water outlet An Dan >When 3mg/L, DO is improved, improves be no more than 15% every time, every time adjustment interval at least 4h.
8. a kind of low ratio of carbon to ammonium biological carbon and phosphorous removal method according to claim 1, which is characterized in that TP Qu Chushuais >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 of returned sludge contains
Phosphorus Shuai >4%.
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