CN104986857B - A kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge installation for fermenting and method - Google Patents
A kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge installation for fermenting and method Download PDFInfo
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Abstract
A kind of apparatus and method of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge fermentation, belong to city domestic sewage biologic treating technique field.The system includes former pond, A/O reactors, second pond, intermediate water tank, storage basin, excess sludge fermentation coupling denitrification synchronous anaerobic ammoxidation autotrophic denitrification sequencing batch reactor (SFDA SBR), computer；Former pond is connected with A/O reactors water inlet end with SFDA SBR water inlet end respectively, and the note mud end of the spoil disposal end of second pond respectively with the first cell compartment returned sludge end of A/O reactors and storage basin is connected, and the spoil disposal end of storage basin is connected with SFDA SBR note mud end.Its method is：Low C/N enters A/O reactors by former pond first than city domestic sewage and carries out nitration reaction and dephosphorization, and A/O reactors are drained into intermediate water tank, then enters SFDA SBR together than sanitary sewage with excess sludge and low C/N.The present invention is advantageously implemented advanced nitrogen, the organic matter that required carbon source is produced from excess sludge fermentation, thus the effect with mud decrement.
Description
Technical field
The present invention relates to a kind of device of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge fermentation and side
Method, belongs to city domestic sewage biologic treating technique field.Dephosphorization and nitration reaction are realized in A/O reactors first, then at
The decrement and sewage of sludge are realized in SFDA-SBR under the collective effect of hydrolysis acidification bacterium, denitrifying bacterium and anaerobic ammonia oxidizing bacteria
The efficient removal of total nitrogen.This technology is applied to low C/N ratios (COD mass concentration and the ratio of total nitrogen concentration) city
The advanced treating of city's sanitary sewage.
Background technology
In recent years, eutrophication is on the rise caused by Water, phosphorus are excessive, and water area ecological environment and the mankind are strong
Health, which is received, to be had a strong impact on, and is effluent quality of this China to municipal sewage plant, and the nitrogen, phosphorus index especially to water outlet will
Ask stricter.Bio-denitrification technology is current most widely used sewage water denitrification technology, and principle is to pass through nitrifier and anti-nitre
Change the removal that nitrogen is realized in bacterium effect, but it reaches that the key of efficient denitrification is sufficient carbon source.
China's major part city domestic sewage, the problem of there is carbon source wretched insufficiency, the carbon source of its own can not meet de-
The demand of nitrogen, and then as Sewage Biological Treatment total nitrogen key reason not up to standard.Domestic existing sewage biological treatment system is past
Toward by adding the outer carbon source such as methanol come supplementary carbon source demand, this both adds processing cost, and CO in water factory is exacerbated again2Row
Put a large amount of generations with excess sludge.Further, since the excess sludge production of sewage biological treatment system is big, processing cost is high
High, for a typical urban sewage treatment system, its Treatment of Sludge cost constitutes about the 40% of totle drilling cost, and remaining
The processing disposal of sludge easily causes the secondary release of nutrient, easily causes secondary pollution.
Anaerobic ammonia oxidation process is a kind of bio-denitrifying sewage approach of economical and efficient, its principle under anoxic conditions,
Anaerobic ammonia oxidizing bacteria, using nitrite nitrogen as electron acceptor, is nitrogen directly by ammonium oxidation, compared with traditional handicraft, anaerobism ammonia oxygen
Chemical industry skill is without oxygen supply and organic carbon source, and surplus sludge volume is low, and anaerobic ammonia oxidizing bacteria metabolic activity is high, process volume conversion ratio
It is high.But Anammox reaction is using nitrite as matrix, it usually needs be used as pre-treating technology using short distance nitration.Short distance nitre
The realization of change is generally required makes nitration reaction only proceed to nitrous by limiting dissolved oxygen, free ammonia suppression and hot operation etc.
This step of state nitrogen, but in low practical applications of the C/N than city domestic sewage is handled, because nitrite accumulation is difficult to maintain
Stable and sewage warming temperature is more difficult and the condition such as being not suitable for economically, and short distance nitration is often subject to limitation.
The content of the invention
In order to solve the above problems, the present invention proposes that a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint is remaining dirty
The apparatus and method of mud fermentation, nitration reaction and the dephosphorization of sewage are carried out in A/O reactors, is sent out subsequently through external source sludge
Ferment, denitrification and Anammox carry out the advanced nitrogen of sewage, and can realize mud decrement simultaneously.
To achieve the above object, the present invention provides a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge
The device of fermentation, including former pond (1), A/O reactors (2), raw water intake pump I (2.1), agitating device I (2.2), aeration head
(2.3), air compressor (2.4), gas flowmeter (2.5), second pond (3), drainpipe (3.1), sludge reflux pump (3.2),
Residual sludge pump (3.3), intermediate water tank (4), storage basin (5), SFDA-SBR (6), nitrification liquid intake pump (6.1), raw water water inlet
Pump II (6.2), enter dredge pump (6.3), agitating device II (6.4), computer automatic control system (7), pH processes on-line monitoring control
Device (7.1) processed, ORP process Online Monitoring Control devices (7.2), pH probes (7.3), ORP probes (7.4), temperature control heating rod
(7.5), temperature monitor and control device (7.6).
Former pond (1) by raw water intake pump I (2.1) and raw water intake pump II (6.2) respectively with A/O reactors (2)
Water inlet end and SFDA-SBR (6) water inlet end connection；In A/O reactors (2) provided with agitating device I (2.2), aeration head (2.3),
Air compressor (2.4), gas flowmeter (2.5)；The discharge ends of A/O reactors (2) are connected with the injection end of second pond (3),
The draining of second pond (3) flows into intermediate water tank (4) by drainpipe (3.1), and the spoil disposal end of second pond (3) passes through sludge reflux pump
And residual sludge pump (3.3) sludge reflux end respectively with the first cell compartment in A/O reactors (2) anaerobic zone and storage basin (5) (3.2)
Note mud end connection；The water side of intermediate water tank (4) is connected by nitrification liquid intake pump (6.1) and SFDA-SBR (6) water injection end
Connect, the spoil disposal end of storage basin (5) is connected by entering dredge pump (6.3) with SFDA-SBR (6) mud inlet end.SFDA-SBR (6) is internal
PH probes (7.3), ORP probes (7.4) and temperature control heating rod (7.5) are set, respectively with pH process Online Monitoring Control devices
(7.1), ORP processes Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) connection, controller are automatic with computer
Control system (7) is connected.
A/O reactors (2) are divided into 6-9 cell compartment with the dividing plate for the water hole that is staggered up and down, be provided be connected according to this
Anaerobic zone cell compartment and aerobic zone cell compartment, anaerobic zone cell compartment is divided into 2-3 cell compartment, is provided with agitating device I (2.2), aerobic zone
Cell compartment is divided into 4-6 cell compartment, is provided with aeration head (2.3), and air is provided by air compressor (2.4).
Agitating device II (6.4), pH probe (7.3), ORP probes (7.4) and temperature control heating are set inside SFDA-SBR (6)
Rod (7.5), probe and heating rod pass through pH process Online Monitoring Control devices (7.1), ORP process Online Monitoring Control devices respectively
(7.2) it is connected with temperature monitor and control device (7.6) with computer automatic control system (7).Computer automatic control system (7) leads to
Online Monitoring Control device is crossed by SFDA-SBR internal temperature controls at 30 DEG C, the pH at any of which moment, ORP, temperature are shown in
On computer display, and pH, ORP change in process curve can be drawn automatically.
Present invention simultaneously provides a kind of method of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge fermentation,
Comprise the following steps：
(1) A/O reactors are started：A/O reactors are injected by seed sludge of the sludge from final clarifier of municipal sewage plant,
Its sludge concentration is 2000-4000mg/L, meanwhile, former pond is injected as raw water than city domestic sewage using low C/N, passes through original
Water intake pump I is squeezed into A/O reactors；Subsequent start-up stirring system and aerating system, A/O reactors anaerobic zone cell compartment are put
Phosphorus reaction, aerobic zone cell compartment occurs DO in nitrification suction phosphorus reaction, course of reaction and maintains 2-3mg/L, and regulation flow of inlet water makes A/O
Hydraulic detention time of the reactor anaerobic zone per cell compartment is 0.5h~1.0h, and hydraulic detention time of the aerobic zone per cell compartment is 1.0h
~2.0h, the hydraulic detention time of second pond is 1.0h~1.5h, opens sludge reflux pump and residual sludge pump, and conditioning of mud is returned
Stream is than being 50%~100%.
(2) SFDA-SBR is started：SFDA-SBR startup is divided into three phases, and/anoxic sludge system is detested in stage one, inoculation
Sludge, its sludge concentration be 3000~4000mg/L, using sodium acetate, sodium nitrate mixed solution be used as raw water add SFDA-
The mass ratio of carbon and nitrogen is 2~3 in SBR, mixed liquor, stirs under anoxic conditions, observes that pH constantly subtracts in reactor
Speed rises, and ORP constantly slows down, but ORP value is consistently greater than -300mV, stable operation to nitrous accumulation rate reach 80% with
On, realize the domestication culture of part denitrification sludge；In the stage two, the amount of sodium acetate in water inlet is reduced, with municipal sewage treatment
Plant excess sludge replaces reduced sodium acetate, increases the input amount of excess sludge, until sodium acetate is all substituted by excess sludge.
Volatile fatty acid (VFAs) the substituted acetic acid sodium produced that fermented using excess sludge is used as denitrifying carbon source.Inject sodium hydroxide
Solution controls pH in reactor to be 8.0~9.0, is 30 DEG C by temperature in heating rod maintenance reaction device, realizes denitrification and surplus
The coupling of remaining sludge fermentation.Sodium nitrate solution is replaced as water inlet with the nitrification liquid of A/O reactor water outlets so that final nitrous product
Tired rate still reaches more than 80%；Stable operation is inoculated with stage three, the SFDA-SBR coupled that fermented to denitrification and excess sludge
The anaerobic ammonium oxidation sludge of more than ten months make it that sludge concentration is 5000~6000mg/L in reactor.To low C/N than living
The water outlet nitrification liquid of A/O reactors is added in sewage so that the mass ratio of ammonia nitrogen and nitrate nitrogen is 1:1.5~1:10, made with this
For water inlet injection SFDA-SBR, when in SFDA-SBR TN clearances higher than 90% and persistently maintain more than 15 days when, reach residue
The realization of sludge fermentation coupling denitrification synchronous anaerobic ammoxidation autotrophic denitrification.
(3) series operation A/O reactors and SFDA-SBR：Low C/N in raw water box is intake than sanitary sewage by raw water
Pump I squeezes into A/O reactors, and sludge concentration is 2000-3000mg/L, subsequent start-up agitating device I, and adjusting gas flow meter makes molten
Solution oxygen maintains 2-3mg/L；A/O reactor water outlets enter after second pond, mud-water separation, and precipitating sludge is back to A/O reactors
The first cell compartment in anaerobic zone sludge reflux end, reflux ratio control in 50%-100%, supernatant pass through outlet pipe flow into the middle of water
Case, opens connection SFDA-SBR two intake pumps, adjusts pump speed so that raw water, which enters water volume and enters water volume ratio with nitrification liquid, is
1:1.5~1:10, it is the 3/5~4/5 of SFDA-SBR dischargeable capacitys always to enter water volume, meanwhile, it is fresh remaining dirty in storage basin
Mud is injected in SFDA-SBR by entering dredge pump, adjusts pump speed, enters the 1/5-2/5 that mud volume is SFDA-SBR dischargeable capacitys, water inlet
Enter mud time 0.5h, anoxia stirring 4.5h, precipitate 1h, draining 0.25h, draining ratio is 0.5~0.7,1-2 week of operation daily
Phase.
The technical principle of the present invention is as follows：
Low C/N initially enters A/O reactors than city domestic sewage, in anaerobic zone, and polyP bacteria under anaerobic, is decomposed
Internal polyphosphate produces ATP, and sewage mesostroma is absorbed into intracellular synthesis PHB in active transport mode using ATP,
Simultaneously discharge phosphate in environment, abbreviation anaerobic phosphorus release reaction, subsequently enter aerobic zone, polyP bacteria under aerobic condition,
PHB and Exogenous ground substance in disassembler body, produce proton motive force and external phosphate are transported into synthesis ATP and core in vivo
Acid, storage of cells thing is aggregated into by superfluous phosphate, and abbreviation aerobic phosphorus absorption is reacted, while under aerobic condition, in nitrosation
It is nitrite nitrogen by the ammonia nitrogen initial oxidation in sewage in the presence of bacterium and nitrifier, then reoxidizes as nitrate nitrogen, referred to as nitrification
Reaction；Nitrification liquid enters SFDA-SBR, in the reactor on the one hand, the carbon source that denitrifying bacterium can be produced using excess sludge fermentation
It is nitrite nitrogen by the nitrate nitrogen part denitrification produced in the nitrate nitrogen and anaerobic ammonium oxidation process in nitrification liquid, moreover it is possible to will be
Remaining nitrate nitrogen and nitrite nitrogen are reduced to nitrogen and removed from system in system；On the other hand, anaerobic ammonia oxidizing bacteria is utilized
Autotrophic denitrification ability, the Asia of the ammonia nitrogen in raw water and excess sludge the are fermented ammonia nitrogen produced and the generation of part denitrification
Nitre is converted into nitrogen and removed from system, so that the advanced nitrogen of whole system is realized, while making excess sludge obtain effective profit
With realizing mud decrement.The present invention it is critical that tame out part denitrifying bacterium with Aquaponic by using low C/N ratios, make Asia
Nitre accumulation rate is stably maintained at more than 80%, so that it is guaranteed that the ammoxidation of excess sludge fermentation coupling unit denitrification synchronous anaerobic is certainly
Supporting anaerobic ammonia oxidizing bacteria in denitrification system has enough substrates.
Compared with prior art, the present invention has advantages below：
1st, by the way that excess sludge is fermented, denitrification and Anammox autotrophic denitrification are organically combined, and realize that low C/N compares city
The advanced nitrogen and excess sludge reduction of city's sanitary sewage, reach that saving sewage water denitrification carbon source adds the purpose with processing cost；
2nd, due to microbial population in excess sludge fermentation coupling denitrification synchronous anaerobic ammoxidation self-supported denitrification reactor
With diversity, even if variation water quality is very big once in a while for city domestic sewage, the efficient removal of total nitrogen can be still realized, i.e., the system can
To successfully manage nitrogen load impact；
3rd, realize the minimizing processing of bio-denitrifying sewage system self residual sludge and utilize, improve mud and sewage processing
Efficiency, saves processing cost and floor space.
4th, whole technological operation is simple, when only need to set the reaction in flow of inlet water and SFDA-SBR each stage of two reactors
Between, without complicated control process, water outlet TN can meet discharge standard.
Brief description of the drawings
Fig. 1 is the structure chart of apparatus of the present invention.
Primary symbols are described as follows：
1- former pond 2-A/O reactor 3- second ponds
4- intermediate water tank 5- storage basins
6- excess sludges fermentation coupling denitrification synchronous anaerobic ammoxidation autotrophic denitrification SBR
2.1- raw water intake pump 2.2- agitating device I 2.3- aeration heads
2.4- air compressor 2.5- gas flowmeter 3.1- nitrification liquid outlet pipes
3.2- sludge reflux pump 3.3- residual sludge pump 6.1- nitrification liquid intake pumps
6.2- raw water intake pumps 6.3- enters dredge pump 6.4- agitating devices II
7.1-pH process Online Monitoring Control device 7.2-ORP process Online Monitoring Control devices
7.3-pH probe 7.4-ORP probe 7.5- temperature control heating rods
7.6- on-line temperature monitoring controllers
Embodiment
The present invention is described in further detail in conjunction with the accompanying drawings and embodiments.
As shown in figure 1, a kind of device of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge fermentation, including
Former pond (1), A/O reactors (2), raw water intake pump I (2.1), agitating device I (2.2), aeration head (2.3), air compressor
(2.4), gas flowmeter (2.5), second pond (3), drainpipe (3.1), sludge reflux pump (3.2), residual sludge pump (3.3),
Intermediate water tank (4), storage basin (5), SFDA-SBR (6), nitrification liquid intake pump (6.1), raw water intake pump II (6.2), enter dredge pump
(6.3), agitating device II (6.4), computer automatic control system (7), pH process Online Monitoring Control devices (7.1), ORP processes
Online Monitoring Control device (7.2), pH probes (7.3), ORP probes (7.4), temperature control heating rod (7.5), temperature monitor and control device
(7.6)。
Former pond (1) by raw water intake pump I (2.1) and raw water intake pump II (6.2) respectively with A/O reactors (2)
Water inlet end and SFDA-SBR (6) water inlet end connection；In A/O reactors (2) provided with agitating device I (2.2), aeration head (2.3),
Air compressor (2.4), gas flowmeter (2.5)；The discharge ends of A/O reactors (2) are connected with the injection end of second pond (3),
The draining of second pond (3) flows into intermediate water tank (4) by drainpipe (3.1), and the spoil disposal end of second pond (3) passes through sludge reflux pump
And residual sludge pump (3.3) sludge reflux end respectively with the first cell compartment in A/O reactors (2) anaerobic zone and storage basin (5) (3.2)
Note mud end connection；The water side of intermediate water tank (4) is connected by nitrification liquid intake pump (6.1) and SFDA-SBR (6) water injection end
Connect, the spoil disposal end of storage basin (5) is connected by entering dredge pump (6.3) with SFDA-SBR (6) mud inlet end.SFDA-SBR (6) is internal
PH probes (7.3), ORP probes (7.4) and temperature control heating rod (7.5) are set, respectively with pH process Online Monitoring Control devices
(7.1), ORP processes Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) connection, controller are automatic with computer
Control system (7) is connected.
A/O reactors (2) are divided into 6-9 cell compartment with the dividing plate for the water hole that is staggered up and down, be provided be connected according to this
Anaerobic zone cell compartment and aerobic zone cell compartment, anaerobic zone cell compartment is divided into 2-3 cell compartment, is provided with agitating device I (2.2), aerobic zone
Cell compartment is divided into 4-6 cell compartment, is provided with aeration head (2.3), and air is provided by air compressor (2.4).
Agitating device II (6.4), pH probe (7.3), ORP probes (7.4) and temperature control heating are set inside SFDA-SBR (6)
Rod (7.5), probe and heating rod pass through pH process Online Monitoring Control devices (7.1), ORP process Online Monitoring Control devices respectively
(7.2) it is connected with temperature monitor and control device (7.6) with computer automatic control system (7).Computer automatic control system (7) leads to
Online Monitoring Control device is crossed by SFDA-SBR internal temperature controls at 30 DEG C, the pH at any of which moment, ORP, temperature are shown in
On computer display, and pH, ORP change in process curve can be drawn automatically.
Specific experiment case is as follows：
Specific test water is using Beijing University of Technology's dependents' district sanitary sewage as raw water, and specific water quality is as follows：COD is dense
Spend for 180-300mg/L, NH4 +- N concentration is 50-85mg/L, NO2 -- N and NO3 -- N is below test limit, and COD/N ratios are 2.2
~3.5, belong to typical low C/N and compare sewage.A/O reactors dischargeable capacity used is 9L, is divided into 6 cell compartments, and preceding two cell compartment is anaerobism
Area, rear four cell compartment is aerobic zone, and the water flowing duct up and down staggeredly that each cell compartment is arranged on along water (flow) direction on each dividing plate is connected, its
Total hrt is 8h, and the wherein anaerobism time is 2h, and aerobic time is 6h.SFDA-SBR used dischargeable capacity is 10L,
Draining ratio is 0.6, daily 2 cycles of operation, and each cycle includes water inlet 0.5h, stirs 4.5h, precipitates 1.0h, draining 0.25h.
Carrying out practically process is as follows：
(1) it is fresher with municipal sewage plant than city domestic sewage with filling low C/N in storage basin respectively to former pond
Excess sludge.
(2) A/O reactors carry out nitrification and phosphorus removal processing：A/O reactors seed sludge is municipal sewage plant's second pond
Spoil disposal, with good denitrogenation dephosphorizing ability, the low C/N ratios city domestic sewage injected in seed sludge and former pond is mixed
Formed in 2500mg/L mixed liquor, injection A/O reactors and second pond.Agitating device, air pressure in unlatching A/O reactors
Contracting machine, adjusting gas flow meter controls the DO concentration in A/O reactors between 2~3mg/L.A/O intake pumps are opened to start
To injecting low C/N in A/O reactors than city domestic sewage, while starting sludge reflux pump and residual sludge pump, sludge reflux
Than for 60%, starting the nitrification and phosphorus removal processing procedure of A/O reactors.
(3) in nitrification and phosphorus removal processing procedure, maintain the ammonia oxidation rate of A/O water outlets more than 85%, wherein nitrate nitrogen is accumulated
Tired rate is more than 90%, and adjusts the dissolved oxygen concentration of aerobic zone in A/O reactors with this, while maintaining A/O processing systems
SRT is 30d or so.
(4) treat to fill in intermediate water tank after the nitrification liquid discharged from A/O reactors, open the two of connection SFDA-SBR
Individual intake pump, adjusts pump speed, and it is 1 to make raw water enter water volume to enter water volume ratio with nitrification liquid:6, always enter water volume for SFDA-SBR
The 4/5 of dischargeable capacity, meanwhile, the fresh excess sludge in storage basin is injected in SFDA-SBR by entering dredge pump, is adjusted pump speed, is entered
Mud volume is the 1/5 of SFDA-SBR dischargeable capacitys, intakes into mud time 0.5h, anoxia stirring 4.5h, precipitates 1h, draining 0.25h,
Draining ratio is 0.6, daily 2 cycles of operation.
Before system is continuously run, first SFDA-SBR is started, detailed process was divided into the next stage：Stage one,
/ the sludge of anoxic sludge system is detested in inoculation, and its sludge concentration is 3000~4000mg/L, molten with the mixing of sodium acetate, sodium nitrate
The mass ratio that liquid adds carbon and nitrogen in SFDA-SBR, mixed liquor as raw water is 2~3, is stirred under anoxic conditions, is observed
PH constantly slows down rising in reactor, and ORP is constantly slowed down, but ORP value is consistently greater than -300mV, stable operation to Asia product
Tired rate reaches more than 80%, realizes the domestication culture of part denitrification sludge；In the stage two, the amount of sodium acetate in water inlet is reduced,
Reduced sodium acetate is replaced with excess sludge of municipal sewage plant, increases the input amount of excess sludge, until sodium acetate is whole
Replaced by excess sludge.The volatile fatty acid substituted acetic acid sodium produced that fermented using excess sludge is used as denitrifying carbon source.Note
Entering sodium hydroxide solution controls pH in reactor to be 8.0~9.0, is 30 DEG C by temperature in heating rod maintenance reaction device, realizes
Denitrification and the coupling of excess sludge fermentation.Sodium nitrate solution is replaced as water inlet with the nitrification liquid of A/O reactor water outlets so that
Final nitrous accumulation rate still reaches more than 80%；Connect in stage three, the SFDA-SBR coupled that fermented to denitrification and excess sludge
The anaerobic ammonium oxidation sludge for planting stable operation more than ten months make it that sludge concentration is 5000~6000mg/L in reactor.To low
Water outlet nitrification liquids of the C/N than adding A/O reactors in sanitary sewage so that the mass ratio of ammonia nitrogen and nitrate nitrogen is 1:1.5~
1:10, using this mixed liquor as SFDA-SBR water inlet, when TN clearances are higher than 90% in SFDA-SBR and persistently maintain 15 days
During the above, the realization of excess sludge fermentation coupling denitrification synchronous anaerobic ammoxidation autotrophic denitrification is reached.
The excess sludge fermentation synchronization low C/N of advanced treating handles low C/N than the device of city domestic sewage and compares urban life
Sewage, the pH value of final outflow water is 7.2-7.6, ammonia nitrogen concentration 1.2-6.7mg/L, total nitrogen concentration 10-20mg/L, COD value 40-
60mg/L, while mud decrement about 30%.
Claims (2)
1. a kind of processing unit of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing joint excess sludge fermentation, it is characterised in that：
Including former pond (1), A/O reactors (2), raw water intake pump I (2.1), agitating device I (2.2), aeration head (2.3), air pressure
Contracting machine (2.4), gas flowmeter (2.5), second pond (3), drainpipe (3.1), sludge reflux pump (3.2), residual sludge pump
(3.3), intermediate water tank (4), storage basin (5), SFDA-SBR (6), nitrification liquid intake pump (6.1), raw water intake pump II (6.2),
Enter dredge pump (6.3), agitating device II (6.4), computer automatic control system (7), pH process Online Monitoring Control devices (7.1),
ORP process Online Monitoring Control devices (7.2), pH probes (7.3), ORP probes (7.4), temperature control heating rod (7.5), temperature monitoring
Controller (7.6)；
Water inlet of the former pond (1) by raw water intake pump I (2.1) and raw water intake pump II (6.2) respectively with A/O reactors (2)
End and SFDA-SBR (6) water inlet end are connected；Agitating device I (2.2), aeration head (2.3), air are provided with A/O reactors (2)
Compressor (2.4), gas flowmeter (2.5)；The discharge ends of A/O reactors (2) are connected with the injection end of second pond (3), and two sink
The draining in pond (3) flows into intermediate water tank (4) by drainpipe (3.1), and the spoil disposal end of second pond (3) passes through sludge reflux pump
And residual sludge pump (3.3) sludge reflux end respectively with the first cell compartment in A/O reactors (2) anaerobic zone and storage basin (5) (3.2)
Note mud end connection；The water side of intermediate water tank (4) is connected by nitrification liquid intake pump (6.1) and SFDA-SBR (6) water injection end
Connect, the spoil disposal end of storage basin (5) is connected by entering dredge pump (6.3) with SFDA-SBR (6) mud inlet end；SFDA-SBR (6) is internal
PH probes (7.3), ORP probes (7.4) and temperature control heating rod (7.5) are set, respectively with pH process Online Monitoring Control devices
(7.1), ORP processes Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) connection, controller are automatic with computer
Control system (7) is connected；
A/O reactors (2) are divided into 6-9 cell compartment with the dividing plate of water hole of being staggered up and down, and detesting of being connected is provided with according to this
Oxygen area cell compartment and aerobic zone cell compartment, anaerobic zone cell compartment are divided into 2-3 cell compartment, are provided with agitating device I (2.2), aerobic zone cell compartment
It is divided into 4-6 cell compartment, is provided with aeration head (2.3), air is provided by air compressor (2.4)；
Agitating device II (6.4), pH probe (7.3), ORP probes (7.4) and temperature control heating rod are set inside SFDA-SBR (6)
(7.5), probe and heating rod pass through pH process Online Monitoring Control devices (7.1), ORP process Online Monitoring Control devices respectively
(7.2) it is connected with temperature monitor and control device (7.6) with computer automatic control system (7)；Computer automatic control system (7) leads to
Online Monitoring Control device is crossed by SFDA-SBR internal temperature controls at 30 ± 1 DEG C, the pH at any of which moment, ORP, temperature are shown
On computer display, and pH, ORP change in process curve can be drawn automatically.
2. the method for application claim 1 described device, it is characterised in that comprise the following steps：
(1) A/O reactors are started：A/O reactors are injected by seed sludge of the sludge from final clarifier of municipal sewage plant, it is dirty
Mud concentration is 2000-4000mg/L, meanwhile, former pond is injected as raw water than city domestic sewage using low C/N, entered by raw water
Water pump I is squeezed into A/O reactors；Subsequent start-up stirring system and aerating system, it is anti-that A/O reactors anaerobic zone cell compartment puts phosphorus
Should, aerobic zone cell compartment occurs DO in nitrification suction phosphorus reaction, course of reaction and maintains 2-3mg/L, and regulation flow of inlet water reacts A/O
Device anaerobic zone per cell compartment hydraulic detention time be 0.5h~1.0h, aerobic zone per cell compartment hydraulic detention time for 1.0h~
2.0h, the hydraulic detention time of second pond is 1.0h~1.5h, opens sludge reflux pump and residual sludge pump, conditioning of mud backflow
Than for 50%~100%；
(2) SFDA-SBR is started：SFDA-SBR startup is divided into three phases, the stage one, and inoculation detests/dirt of anoxic sludge system
Mud, its sludge concentration is 3000~4000mg/L；Using sodium acetate, sodium nitrate mixed solution as raw water add SFDA-SBR,
The mass ratio of carbon and nitrogen is 2~3 in mixed liquor, is stirred under anoxic conditions, is observed in reactor in pH constantly decelerations
Rise, ORP is constantly slowed down, but ORP value is consistently greater than -300mV, and stable operation to nitrous accumulation rate reaches more than 80%, in fact
The domestication culture of part denitrification sludge is showed；In the stage two, the amount of sodium acetate in water inlet is reduced, it is remaining with municipal sewage plant
Sludge replaces reduced sodium acetate, increases the input amount of excess sludge, until sodium acetate is all substituted by excess sludge；With residue
The volatile fatty acid substituted acetic acid sodium that sludge fermentation is produced is used as denitrifying carbon source；Inject sodium hydroxide solution control reaction
PH is 8.0~9.0 in device, is 30 DEG C by temperature in heating rod maintenance reaction device, realizes what denitrification and excess sludge fermented
Coupling；Sodium nitrate solution is replaced as water inlet with the nitrification liquid of A/O reactor water outlets so that final nitrous accumulation rate still reaches
More than 80%；Inoculation stable operation more than ten months in stage three, the SFDA-SBR coupled that fermented to denitrification and excess sludge
Anaerobic ammonium oxidation sludge cause in reactor sludge concentration to be 5000~6000mg/L；To low C/N than being added in sanitary sewage
The water outlet nitrification liquid of A/O reactors so that the mass ratio of ammonia nitrogen and nitrate nitrogen is 1:1.5~1:10, injected in this, as water inlet
SFDA-SBR, when in SFDA-SBR TN clearances higher than 90% and persistently maintain more than 15 days when, reach excess sludge ferment coupling
Close the realization of denitrification synchronous anaerobic ammoxidation autotrophic denitrification；
(3) series operation A/O reactors and SFDA-SBR：Low C/N in raw water box is beaten than sanitary sewage by raw water intake pump I
Enter A/O reactors, sludge concentration is 2000-3000mg/L, and subsequent start-up agitating device I, adjusting gas flow meter makes dissolved oxygen
Maintain 2-3mg/L；A/O reactor water outlets enter after second pond, mud-water separation, and precipitating sludge is back to detesting for A/O reactors
The sludge reflux end of oxygen area head cell compartments, reflux ratio control flows into intermediate water tank by outlet pipe, opened in 50%-100%, supernatant
Connection SFDA-SBR two intake pumps are opened, pump speed is adjusted so that it is 1 that raw water, which enters water volume and enters water volume ratio with nitrification liquid,:1.5
~1:10, it is the 3/5~4/5 of SFDA-SBR dischargeable capacitys always to enter water volume, meanwhile, the fresh excess sludge in storage basin passes through
Enter in dredge pump injection SFDA-SBR, adjust pump speed, enter the 1/5-2/5 that mud volume is SFDA-SBR dischargeable capacitys, when intaking into mud
Between 0.5h, anoxia stirring 4.5h, precipitate 1h, draining 0.25h, draining ratio be 0.5~0.7, daily operation 1-2 cycle.
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| CN108585202B (en) * | 2018-05-14 | 2021-04-30 | 北京工业大学 | Process for realizing partial short-cut nitrification, sludge fermentation coupling denitrification and anaerobic ammonia oxidation treatment of domestic sewage in sequencing batch reactor |
| CN108862581A (en) * | 2018-07-04 | 2018-11-23 | 北京工业大学 | A kind of device and method that AO biomembrane+sludge fermentation coupling denitrification realizes sewage deep denitrogenation synchronous sludge decrement |
| CN109879420A (en) * | 2019-03-04 | 2019-06-14 | 西安建筑科技大学 | A kind of carbon source prepares-stores integrated rural sewage-treatment plant and method |
| CN110002592B (en) * | 2019-05-05 | 2021-09-14 | 北京工业大学 | Device and method for treating domestic sewage by coupling short-cut denitrification-sludge fermentation with anaerobic ammonia oxidation system |
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