CN107032498A - The method that batch enters enhanced water SBR technique deep denitrifications - Google Patents
The method that batch enters enhanced water SBR technique deep denitrifications Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/04—Oxidation reduction potential [ORP]
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/42—Liquid level
Abstract
The method that batch enters enhanced water SBR technique deep denitrifications belongs to technical field of sewage, it is adaptable to nitrogenous organic industrial sewage advanced nitrogen processing.The total Water point n times (n >=3) of SBR period treatments is filled with reactor by the present invention, is aerated 1 water-filling stirring/aeration of →... n → n water-filling according to 1 water-filling stirring/aeration → 2 time water-filling is stirred/and is added proper amount of carbon source stirring → short-time aeration, precipitation, draining, spoil disposal, idle mode and runs.Each filled water amount is determined according to processed raw water quality, denitrogenation target, total water-filling ratio and water-filling frequency n.By every section of aerobic nitrification process of pH, DO On-line Control, by every section of stirring denitrification process of pH On-line Controls.The present invention can reasonable distribution enter Organic substance in water to denitrification section, promote denitrification process using ammonia nitrogen in water inlet, the basicity for producing denitrification adds to nitration section, the part ammonia nitrogen in water-filling is removed without aerobic section in denitrification, and then realize synergy, energy-conservation, consumption reduction and advanced nitrogen purpose.
Description
Technical field
The invention belongs to technical field of sewage, and in particular to a kind of batch enters enhanced water SBR technique deep denitrifications
Method.
Background technology
Body eutrophication problem causes people's common concern in recent years, and nitrogen is the principal element for causing body eutrophication
One of.Current technology nitric efficiency how is improved, the new denitrogenation technology and new technology of economical and efficient is researched and developed, is urgently to be resolved hurrily
Important topic, while this is also one of key problem of stain disease advanced treating research.
Bioanalysis is cost-effective stain disease denitrifying method generally acknowledged at present.Wide variety of life in current engineering
Thing denitrification process is still built upon the group technology in traditional biological denitrogenation theoretical foundation, and the space such as using A/O as representative is suitable
Sequence continuous flow process and the time sequencing piston-flow process by representative of SBR.Particularly SBR techniques, due to the spirit of its method of operation
It is living, aerobic, anoxic and the alternate environmental condition of anaerobic state can be realized as needed, it has also become more had with respect to continuous flow process
The denitrification process of advantage.
According to traditional theory, biological denitrification process mainly includes two-step reaction process, that is, first passes through aerobic nitrification
It is nitrate nitrogen (nitrate nitrogen and nitrite nitrogen) by ammonium oxidation, then again by the denitrification of anoxic, with organic matter
By nitrate-nitrogen reduction it is nitrogen for electron donor, final nitrogen is escaped from water.In nitrifying process, it is nitre often to aoxidize 1g ammonia nitrogens
Hydrochlorate nitrogen will consume 7.14g basicity (with CaCO3Meter), 1g nitrate nitrogens are often reduced in denitrification process for nitrogen, can be produced
Raw 3.57g basicity is (with CaCO3Meter).
When carrying out advanced nitrogen using SBR techniques, its basic method of operation is typically：Raw water enters after system, first leads to
Aerobic aeration operation, the organic matter gone in water removal are crossed, and is nitrate nitrogen by ammonium oxidation；Then again by adding appropriate carbon
Source, under conditions of anoxia stirring, completes the denitrification denitrogenation course of reaction that nitrate-nitrogen reduction is nitrogen.Deposit in this course
Subject matter be：
(1) in order to realize advanced nitrogen, denitrification needs additional carbon；
(2) nitrifying process will consume basicity and cause system pH value to decline, when the basicity relative deficiency in processed raw water,
Need to supplement basicity into raw water；
(3) system operation complex management, and traditional set time program controlled mode, it is difficult to according to the reality of influent quality
Border situation of change adjusts operational factor in time, reaches stable effluent quality.
Nitrifying process based on biological denitrificaion has good phase with pH, dissolved oxygen (DO) and oxidation-reduction potential (ORP)
Guan Xing, denitrification process also has the principle of good correlation with pH and ORP, and in recent years, domestic and foreign scholars are to SBR methods in nitrification
Extensive research has been carried out with the changing rule of pH, DO and ORP in denitrification process.Unanimously think, can with pH, DO and
ORP and is realized with these parameters as the On-line Control parameter of SBR method denitrification process and is terminated (NH in nitration reaction4 +-N≈
When 0mg/L) terminating (nitrate nitrogen ≈ 0mg/L) with anti-nitration reaction, stop aerobic aeration in real time and the denitrogenation of anoxia stirring is online
Control.The achievement in research, although can realize that the adaptive of SBR denitrification process automatically controls, but can not solve well
The problem of basicity being required supplementation with when basicity is not enough in above-mentioned carbon source problem and raw water.
Discovery is studied recently by this seminar, in denilrification system if there is have ammonia and nitrogen components (ammonia nitrogen amount should be greater than by
Deoxidization, degradation nitrate nitrogen amount more than 9%), denitrification denitrogenation speed can be significantly improved, and in denitrification degraded nitrate nitrogen
During, moreover it is possible to while degraded accounts for the ammonia and nitrogen components for the nitrate nitrogen amount more than 8% (average) for being reduced degraded.Obviously, above-mentioned base
In the On-line Control control method of pH, DO and ORP for the SBR method advanced nitrogens of parameter, the ammonia nitrogen in denilrification system is always
0mg/L, this will be unable to obtain facilitation of the ammonia nitrogen to denitrification process.
To enable effectively to be assigned to denitrification section into the organic matter in water, while making the alkali that denitrification process is produced
Degree can add to nitration section, and can promote denitrifying denitrogenation process, present invention knot using the ammonia and nitrogen components in water inlet
Closing " method of the On-line Control SBR denitrification process by parameter of pH and DO ", " it is deep that batch enters enhanced water SBR techniques there is provided one kind
Spend the method for denitrogenation ".
The content of the invention
It is integrated with " with pH, DO parameter On-line Control SBR denitrogenations technology " that the present invention is " ammonia nitrogen promotion denitrification phenomenon "
Innovation.
The basic foundation of invention
(1) when appropriate ammonia and nitrogen components (be more than and be reduced degraded nitrate nitrogen amount more than 9%) are there are in denitrification process, energy
Enough denitrification rate is set to have a more substantial increase；
(2) in the anti-nitre system of biological denitrificaion contain ammonia nitrogen when, denitrification process in addition to deoxidization, degradation nitrate nitrogen composition,
The ammonia and nitrogen components for nitrate nitrogen amount more than 8% (average) that account for being degraded can be also removed simultaneously；
(3) at the end of SBR nitration reactions, obvious characteristic point can occur on pH the and DO duration curves of on-line monitoring
Indicated, obvious characteristic point can also occur at the end of SBR anti-nitration reactions, on the pH duration curves of on-line monitoring gives
To indicate.
Application claims sbr reactor device and its control system have following characteristics
Sbr reactor device is connected with water inlet pipe, carbon source and adds pipe, aeration tube, outlet pipe and discharge pipeline；Sbr reactor device is by entering
Water pump supplies water through water intaking valve, water inlet pipe, adds pump by carbon source and adds valve, carbon source through carbon source and add pipe and adds carbon source, by air blower
It is aerated through being aerated intake valve, aeration tube；Corresponding draining valve and row are also provided with sbr reactor device outlet pipe and discharge pipeline
Slurry valve.
Agitator, liquid level sensor, pH sensors and DO sensors are provided with sbr reactor device；Liquid level sensor and
The detection signal of pH, DO sensor is connected after distinguishing sampled, conversion and processing with process controller, according to system set in advance
System operation control strategy, On-line Control is implemented by the relay in process controller to the running of system.
The operational parameter control of system has：Total water-filling ratio δ in sbr reactor device cycle, water-filling frequency n, each filled water amount
Account for the ratio lambda of cycle total filled water amount1~λn(water-filling scheme) and corresponding filling time τ1~τnAnd the liquid at the end of each water-filling
Position H1~Hn, in aeration process pH and DO signals sampling interval t1, in whipping process pH signals sampling interval t2, denitrification
At the end of pH to the average rate of change K of timepHiValue becomes negative by positive, and keeps KpHi<0 time t3, carbon source add time t4, it is short
When aeration time t5, sedimentation time t6, water discharge time t7, sludge-drainage time t8With standby time t9Deng.
Each procedure of course of reaction, includes the keying of various pumps and valve, and the keying of aeration and stirring system is filled
Water, the process such as carbon source, draining, spoil disposal, idle is added, controlled to complete by control system real-time online all in accordance with control strategy.
Technical scheme
According to above-mentioned basic foundation, basic thought of the invention is：1. by the raw water total amount point of SBR each cycle predetermined process
N times (n >=3) are filled with reactor, are run, utilized the 2 to n-1 times using the water-filling stirring alternate mode of denitrification/aerobic nitrification
Organic matter in water inlet as product-nitrate nitrogen of previous aerobic nitrification section denitrifying carbon source, while utilizing the ammonia in water inlet
Nitrogen promotes the denitrification process of anoxia stirring and reclaims corresponding basicity；2. n-th filled water amount is limited, while adding proper amount of carbon source
Anoxia stirring denitrification；3. it is every by pH parameter On-line Controls by the nitrifying process of each aerobic section of pH and DO parameter On-line Controls
The whipping process of one denitrification section.The purpose of limitation n-th filled water amount is both can to promote denitrification using the ammonia nitrogen in water inlet
Process, can be such that the ammonia nitrogen in n-th water inlet is partially removed in denitrification process without influenceing effluent quality, and take into account again
Certain carbon source is supplemented for this denitrification denitrogenation process (specific water-filling scheme is seen below).
The organic matter that the present invention can be distributed reasonably in water inlet is denitrification denitrogenation service, is promoted using the ammonia nitrogen in water inlet
Denitrification process, while the basicity for enabling denitrification process to produce adds to nitration section, moreover it is possible to make into water part ammonia nitrogen into
Divide and be removed without aerobic nitrification during anoxic denitrification【The ammonia nitrogen amount of removal account for being degraded nitrate nitrogen amount 8% with
Upper (average)】, and then realize the purpose of synergy, energy-conservation, consumption reduction and advanced nitrogen.
The method of operation of sbr reactor device a cycle of the present invention is：【First time water-filling stirring/aeration nitrification】→【Second
Secondary water-filling stirring denitrification/aeration nitrification】→……【(n-1)th water-filling stirring denitrification/aeration nitrification】→【N-th water-filling
And add appropriate carbon source stirring denitrification】→【Short-time aeration】→【Precipitation/draining, spoil disposal/idle】.
Set after system operation control parameter, the basic fundamental for the sbr reactor device a cycle operation that the present invention is provided
Process is as follows：
(1) water-filling stirring operation starts intake pump, while inlet valve and turn on agitator are opened, by pending original
Water is filled with sbr reactor device and stirs operation.When reaching predetermined first time water-filling water (by the filling time τ set1And combine
Liquid level H1Parameter is determined) when, close inlet valve and water inlet water pump in real time by control system, simultaneously close off agitator.
(2) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and goes water removal
In organic matter, and by ammonium oxidation in water be nitrate nitrogen.
In aeration process, real time on-line monitoring pH and DO signal.In the presence of having more organic matter in water inlet, aeration
Initial stage, the pH curves of monitoring are in upward status, and (after first time water-filling in Fig. 2, pH curves were in aeration based on degradation of organic substances
Initial stage is in upward status).After the pH value monitored switchs to stable decline by rising, illustrate that the nitration reaction of denitrogenation has started to just
Often occur, it is approximately platform status that now DO duration curves shape, which also enters, or in the state slowly risen (see Fig. 2).With
The progress of nitration reaction, when the pH curves monitored switch to rise appearance " valley point " (A points in see Fig. 2) by declining, while DO is bent
Line drops to relatively low (general pH in rapid increase state (see B points in Fig. 2), or pH curves<6) switch to be basically unchanged after, simultaneously
When DO values were risen to close to saturation state (belonging to the not enough situation of basicity), show that the nitration reaction of denitrogenation has stopped.Accordingly simultaneously
Binding tests result, the control strategy for formulating aerobic aeration operation is as follows：
Start after aeration, the sampling interval t of the pH and DO signals of on-line monitoring1Take 60s.To eliminate interference, to being gathered
PHiAnd DOiValue carries out the real-time glide filter processing of 4 values (calculating the average value that 4 values are slided), and calculates adjacent two in real time
Individual glide filter value pHLbi-1、pHLbiWith DOLbi-1、DOLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-
ti-1) and KDOi=(DOLbi-DOLbi-1)/(ti-ti-1) value.In aeration process, when monitoring KpHiIt is worth continuous more than 4min<0
Afterwards, note monitoring KpHiAnd KDOiThe situation of value changes, when monitoring KpHiValue is become just (see D points in Fig. 3) by negative, while meeting KDOi
>KDOi-1>KDOi-2>KDOi-3>0 (see E points in Fig. 3), or monitor KpHiAbsolute value<0.002/min, while DOLbi>5mg/L
When, air blower and intake valve are closed by control system in real time, stop aeration operation.
(3) water-filling stirring operation starts intake pump, while water intaking valve and turn on agitator are opened, water-filling stirring operation.When
Reach predetermined water-filling water【By the filling time τ setiAnd combine liquid level Hi(i >=2) parameter is determined】When, by control system
Water intaking valve and water inlet water pump are closed in real time.
In whipping process, denitrifying bacterium is electron donor using the organic matter in water inlet, and denitrification removing upper one is aerobic
Stage produces nitrate nitrogen, while promoting denitrification process using the ammonia nitrogen in water inlet, and also removes in denitrification process part
Ammonia and nitrogen components.
In whipping process, real time on-line monitoring pH signals.After system is stable, due to producing alkali in denitrification process
Degree, the pH duration curves of on-line monitoring can be in stablize propradation (see Fig. 2).With the passage of mixing time, when monitoring pH
When duration curve switchs to stable decline (see C points in Fig. 2) by rising, show that the anti-nitration reaction of denitrogenation has stopped.Accordingly and tie
Result of the test is closed, the control strategy for formulating anoxia stirring operation is as follows：
The sampling interval t of the pH signals of on-line monitoring2Take 60s.For the purposes of eliminating interference, in whipping process, to institute
The pH of collectioniValue carries out the real-time glide filter processing of 4 values (calculating the average value that 4 values are slided), and calculates adjacent two in real time
Individual glide filter value pHLbi-1With pHLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-ti-1).Stirred
Cheng Zhong, when monitoring KpHiIt is worth continuous more than 3min>After 0, start to note monitoring KpHiThe positive and negative situation of change of value.When monitoring
KpHiValue becomes negative (see F points in Fig. 3) by positive, and keeps t3Time (taking 3~4min) above KpHiValue is equal<It is real by control system when 0
When stop stirring operation.
(4) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and goes water removal
Middle possible remaining organic matter, and be nitrate nitrogen by ammonium oxidation in water.
It should be noted that when each cycle the 2nd time and the 2nd later each aeration start, due to the big portion in water inlet
Organic matter is divided to be utilized by denitrification, the organic concentration in system mixed liquor can be relatively low, therefore system can be entered quickly after aeration
Enter normal nitration reaction state, that is, stable decline phenomenon can be occurred in the short period of time by starting pH value after aeration.This with
1st aeration pH at initial stage situation of change can be different (see Fig. 2).
It is real-time by control system when the characteristic point that nitrification end is characterized on pH the and DO duration curves of on-line monitoring occurs
Air blower and intake valve are closed, stopping aeration operation, (control strategy of the 2nd time to (n-1)th aeration process is with the 1st aeration fortune
Capable control strategy).
Stop after aeration operation, system reads water-filling frequency n value set in advance automatically.If the n values read are not reaching to
N-1 water-filling number of times, system will return to process (3) and continue water-filling and stir operation；When reaching (n-1)th water-filling number of times,
System enters process (5) operation.
(5) n-th water-filling and add carbon source stirring operation intake pump and water intaking valve are opened by control system in real time, to anti-
Device is answered to carry out n-th water-filling, carbon source adds valve and carbon source adds pump and adds carbon source (methanol while being opened in real time by control system
Deng), and start agitator stirring operation.When reaching filled water amount and carbon source injected volume (by the filling time τ setnThrown with carbon source
Put time t4And combine liquid level HnParameter determine) when, closed in real time by control system water intaking valve, water inlet water pump and carbon source add pump,
Carbon source adds valve.
The injected volume of carbon source, according in nitrate nitrogen content in mixed liquor at the end of (n-1)th aerobic nitrification and n-th water-filling
Organic matter situation, by being manually adjusted in real time, it is met denitrifying demand (4.0<BOD5/ nitrate nitrogen<4.2).
In whipping process, denitrifying bacterium is electron donor using the organic matter in n-th water inlet and additional carbon source, instead
Nitrification (n-1)th aerobic stage of removing produces nitrate nitrogen, and promotes denitrification process using the ammonia nitrogen in n-th water inlet, simultaneously
Also the ammonia and nitrogen components during n-th is intake are partially removed in denitrification process.When the pH duration curve upper tables of on-line monitoring
When levying the characteristic point that denitrification terminates and occurring【" control strategy of anoxia stirring operation " in the same process of control strategy (3)】, by
Control system stops agitator in real time, stops stirring operation.
(6) operation of short time aeration stops after anoxia stirring, opens air blower and intake valve in real time by control system again
Short time blast aeration (aeration time t is carried out to reactor5Take 7~30min), main purpose is that stripping is attached to mud granule
On nitrogen and further degraded remaining organic matter and remaining part ammonia and nitrogen components may be aoxidized.When the aeration for reaching setting
Time t5When, air blower and intake valve are closed by control system in real time, stop aeration operation.
(7) precipitation stops after short time aeration operation, the mixed liquor in reactor is in precipitated form, realizes muddy water
Separation.
(8) the sedimentation time t of draining and spoil disposal setting to be achieved6When (taking 40~70min), opened in real time by control system
The water discharging valve on drainage pipeline is opened, the supernatant after processing is discharged into reactor；According to the spoil disposal scheme of setting, system is real-time
Open the mud valve spoil disposal on spoil disposal pipeline.As the water discharge time t for reaching setting7(taking 60~90min) and sludge-drainage time t8(take 5
~25min) when, system closes draining valve and mud valve in real time.
(9) reactor that leaves unused is in the holding state that is stopped, when reaching predetermined standby time t9(take 10~
50min) be complete SBR technique a cycles operation process.At this moment, system is transferred to the circular flow in next cycle automatically.
To the explanation of the C/N values (carbon-nitrogen ratio) for the raw water that is processed, basicity and total nitrogen of intaking
In order to obtain the effect of advanced nitrogen, application claims are processed in raw water and are used as denitrifying carbon source containing suitable
Organic matter (BOD5/ total nitrogen>4.0) and the basicity required for biological denitrification process is met【Total alkalinity is (with CaCO3Meter)/kjeldahl nitrogen
>3.6】, the total nitrogen in water based on organic nitrogen and ammonia nitrogen (i.e. kjeldahl nitrogen), and the excursion of kelvin nitrogen concentration for 40~
700mg/L, nitrate nitrogen<4mg/L.
As the relatively low (BOD of C/N values in sewage5/ total nitrogen<4.0), need to be when each denitrification stirs beginning, to reaction when
Supplement adds appropriate outer carbon source in device；When basicity is not enough in sewage【Total alkalinity is (with CaCO3Meter)/kjeldahl nitrogen<3.6】When, should
Appropriate basicity is supplemented to reactor in aeration process, otherwise according to the control strategy of the present invention, though with certain energy-conservation
Synergistic effect, but the purpose of advanced nitrogen can not be realized.
The determination of water-filling scheme
When processed raw water quality meets above-mentioned condition, preceding n-1 water-filling can use equivalent water-filling, in order to obtain
Ammonia nitrogen at least cannot be below the 9.0% of (n-1)th filled water amount to denitrifying facilitation, n-th filled water amount.Meeting denitrogenation
On the premise of handling target, appropriate increase n-th filled water amount advantageously reduces the injected volume and reduction system of the outer carbon source of denitrification
Operating cost.In order to both reach processing target, and preferably energy-conservation, consumption reduction effect can be obtained, the water-filling water of n-th answers root
According to the kelvin nitrogen concentration S of processed raw wateroN, denitrogenation processing target SeN, a cycle total water-filling ratio δ and water-filling frequency n value
It is determined that, the water-filling scheme calculation formula set up according to result of the test is as follows：
Work as λn>λ1~(n-1)When, take λn=λ1~(n-1) (2)
N is a cycle total water-filling number of times (taking 3~4 times) in formula；
λ1~(n-1)The ratio of cycle total filled water amount is accounted for for the 1 to n-1 times filled water amount；
λnThe ratio of cycle total filled water amount is accounted for for n-th filled water amount；
SoNFor the kelvin nitrogen concentration (taking 40~700mg/L) for the raw water that is processed；
SeNFor the total nitrogen concentration (processing target) of water outlet after processing；
δ is total water-filling ratio (taking 1/2~2/3) in sbr reactor device cycle.
Work as λn>λ1~(n-1)When, by λn=λ1~(n-1)(1) formula is brought into obtainThe water-filling ratio of i.e. n times
Example is all equal.
Increase water-filling frequency n value, be conducive to more carbon sources in raw water to be assigned to denitrification section, but which increases be
The complexity of system operation.In actual applications, water-filling frequency n is desirable 3~4 times, total water-filling ratio δ desirable 1/2~2/3.
Water-filling scheme is determined according to the method described above, in laboratory conditions, can obtain preferable denitrogenation processing result.But
In actual production environment, because influence factor is numerous, however not excluded that occur that the denitrogenation processing result of system deviates processing target
SeNSituation.As appearance processing water outlet TN>SeNWhen, can be by λnIt is adjusted by successively decreasing in the way of 2%~0.2%, Zhi Daoman
Foot processing target SeNUntill.
Beneficial effects of the present invention
Now with the kelvin nitrogen concentration S for the raw water that is processedoNFor 100mg/L, nitrate nitrogen is the denitrification carbon in 0mg/L, raw water
Source and basicity are satisfied by biological denitrificaion demand, and processing target is SeN≤ 4mg/L, cycle total water-filling ratio δ of sbr reactor device is 2/
3, exemplified by water-filling frequency n=3 in the cycle of reactor one, to illustrate beneficial effects of the present invention.
According to SoN=100mg/L, SeN=4mg/L, δ=2/3 and n=3, obtained water-filling is calculated by formula (1) and (2)
Scheme is preceding water-filling ratio lambda twice1=λ2=45.4%, the 3rd water-filling ratio lambda3=9.2%.
According to above-mentioned water-filling scheme, " method that batch enters enhanced water SBR technique deep denitrifications " proposed by the present invention and often
Water-filling of rule, aerobic nitrification, outer carbon source anoxia stirring denitrification operation is once added, and ammonia is not present in denitrification section
The system of the SBR denitrogenations of nitrogen compares, with following obvious advantage：
(1) good denitrification effect can be obtained, total nitrogen≤4mg/L of water outlet is realized.
During one 3 water-fillings of cycle, 2 aerobic nitrifications and 2 anoxic denitrification processes are undergone.In whole denitrification process
In：
1. aerobic nitrification process uses pH and DO parameter On-line Controls, it is ensured that nitrifying process ammonium oxidation fills twice
Point；
2. in denitrification process twice, denitrifying carbon source is sufficient, and (the 1st anoxia stirring is using in the 2nd water inlet
Organic matter carry out denitrification, the 2nd anoxia stirring, in addition to the carbon source for having the 3rd water-filling supplement, also additional carbon source), and
And denitrification process uses pH parameter On-line Controls, it is ensured that anoxic denitrification twice is abundant；
3. the 3rd filled water amount is only the 9.2% of a cycle total process water yield, at the end of the 2nd anoxia stirring denitrification,
Part ammonia nitrogen in 3rd water-filling can also be removed, it is ensured that total nitrogen≤4mg/L of final outflow water.
(2) denitrification ability of system can be improved.
Because in the whipping process of denitrification twice in a cycle, appropriate ammonia and nitrogen components are all contained in denilrification system
(exceed nitrate nitrogen amount in system 9%).According to foregoing conclusion, now except normal reduction degraded nitre state in denitrification process
Outside nitrogen component, the ammonia and nitrogen components of the nitrate nitrogen amount more than 8% that is degraded averagely are accounted for while can also increase and remove, therefore improves and is
The denitrification ability of system.
(3) denitrification denitrogenation speed can be made averagely to improve more than 35%, corresponding denitrification stirring power energy consumption is averaged
Reduce more than 25%.
Denitrification denitrogenation speed is set averagely to improve 35% above is the result of a large amount of repetition tests.Because denitrification denitrogenation is fast
The time that rate is stirred with denitrification is inversely proportional, so under the same conditions, containing ammonia nitrogen with being free of the system denitrification of ammonia nitrogen two
Process mixing time than average value will<1/1.35=0.741, therefore the mixing time containing ammonia nitrogen denilrification system can be less
System containing ammonia nitrogen, which averagely reduces by more than (1-0.741)=25.9%, i.e. denitrification whipping process, can averagely save more than 25%.
(4) injected volume of the outer carbon source of denitrification process can significantly be reduced.
Three aspects are mainly manifested in, outer carbon source, this water-filling anoxia stirring are not 1. needed during the 2nd water-filling anoxia stirring
It assume responsibility for the denitrification task of the denitrogenation of whole cycle 45.4%；2. the 3rd filled water amount account for whole cycle processing water ratio be
9.2%, therefore the 3rd water-filling is equivalent to the denitrifying carbon source there is provided in whole process cycle 9.2%；3. repetition test result
Show, the conventional denitrification process that ammonia nitrogen can be relatively free of when denitrification process contains ammonia nitrogen averagely reduces by more than 10% denitrification
Carbon source.This shows, can make 64.6% (45.4%+9.2%+10%) denitrification process without providing outer carbon source.
(5) power consumption of denitrogenation aerobic process can be greatly reduced.
Be mainly manifested in three aspects, 1. in a period treatment raw water more than 54% organic matter (the 2nd filled water amount be
45.4%, the 3rd water is 9.2%, and organic object amount that organic object amount therein is total to be accounted in a period treatment raw water is
54.6%) the anoxia stirring denitrification stage is undergone first, this partial organic substances will largely be utilized by denitrification process, and will be not required to
To pass through aerobic process；2. the ammonia and nitrogen components (averagely accounting for the nitrate nitrogen amount more than 8% that is degraded) that denitrification process is degraded, it is not necessary to
By aerobic nitrification process；3. the organic matter in the 2nd water-filling is mainly utilized by the denitrification of the 1st anoxia stirring, can be subtracted
Influence of the organic matter to the 2nd aerobic nitrification process in light water inlet, this is conducive to the aerobic nitrification speed for improving the 2nd time.Can
See, the aerobic power consumption that these three aspects are reduced is considerable.
(6) can in mitigation system basicity fluctuating range, save the expense that alkali is added when basicity is not enough in water inlet.
Main Basiss：1. alternating oxic-anoxic is run, and the basicity that denitrification process is produced can be made to add to nitration section；②
Aerobic nitre need not be undergone by increasing the ammonia and nitrogen components (averagely accounting for the nitrate nitrogen amount more than 8% that is degraded) of degraded in denitrification process
Change process, this can reduce consumption of the nitrifying process to basicity.Therefore, basicity can fluctuate widely in mitigation system, save into
The expense of alkali is added when basicity is not enough in water.
(7) the aerobic aeration time and anoxia stirring time of biological denitrification process are controlled using real-time online control strategy,
In the absence of nitrification or the incomplete phenomenon of denitrification caused by aeration or mixing time are not enough, also in the absence of because of excess aeration
Or excessive agitation and bring increase operation energy consumption phenomenon.
(8) can be according to the change of raw water quality and system operation situation etc., the operational parameter control of real-time regulating system
And water-filling scheme, obtain on the premise of effluent quality is ensured, it is energy-saving.
(9) it can complete whole processing procedure on-line intelligence control, manage easy to operate.
When the water-filling frequency n in a cycle>When 3, because filled water amount each time will be reduced accordingly, therefore can be further
Basicity fluctuating range in denitrifying carbon source, the ratio and mitigation system that reduce aerobic power consumption is saved in increase.
Brief description of the drawings
Fig. 1 is the operational mode of the SBR technique a cycles of the present invention；
Fig. 2 is that sbr reactor device (is 3 times intake, the 4th inflow is the 3rd inflow according to 4 water inlets for equivalent
15%) in typical cycle pH, DO parameter with ammonia nitrogen and nitrate nitrogen concentration, (nitrite nitrogen concentration is always 0mg/L, not in figure
It is middle represent) change duration curve (DO and pH in figure be through 4 value filterings handle after data)；
Fig. 3 is the rate of change K of pH, DO parameters versus time in Fig. 2pH、KDOWith lasting for ammonia nitrogen and nitrate nitrogen change in concentration
Curve；
Fig. 4 is On-line Control strategic process figure of the invention.
From Fig. 2 and Fig. 3, at the end of each nitrification terminates with denitrification, it can be shown on curve substantially
Characteristic point indicated (in figure institute's marking-up mother at).This is to stop nitrification and denitrification in real time with pH, DO parameter On-line Control
Process provides foundation.
Embodiment
The processed raw water of application claims should be met：Kelvin nitrogen concentration S in raw wateroNExcursion be 40~700mg/
L, nitrate nitrogen<4mg/L；Contain suitable denitrifying carbon source (BOD in raw water5/ total nitrogen>And basicity is sufficient 4.0)【Total alkalinity (with
CaCO3Meter)/kjeldahl nitrogen>3.6】.When basicity is not enough, though the present invention can not realize depth with certain energy efficiency effect
Spend the purpose of denitrogenation.
Embodiment is as follows：
1st step determines system operation control parameter
SBR sewage disposal systems for having been turned on simultaneously stable operation, according to processing target and the processed original grasped
The water quality characteristicses of water, system operation control parameter is determined according to following steps：
(1) total water-filling ratio δ (taking 1/2 to 2/3) and the water-filling frequency n in a cycle (taking 3~4 times) in cycle, root are determined
According to the kelvin nitrogen concentration S of raw wateroNWith processing target SeN, water-filling scheme λ is determined by formula (1) and (2)1~(n- 1) and λn；
(2) the processing water and each water-filling ratio lambda according to a cycle always1~λn, it is determined that each filled water amount, and then
It is determined that corresponding filling time τ every time1~τnWith the liquid level H at the end of each water-filling1~Hn；
(3) the sampling interval t of pH and DO signals in aeration process is determined1The sampling of pH signals in (taking 60s), whipping process
It is spaced t2(taking 60s)；
(4) K at the end of denitrification is determinedpHiValue becomes negative by positive, and keeps KpHi<0 time t3(taking 3~4min)；
(5) the organic matter situation at the end of being nitrified according to (n-1)th time in mixed liquor in nitrate nitrogen content and n-th water-filling,
According to 4.0<BOD5/ nitrate nitrogen<4.2 condition, determines the dosage of the outer carbon source liquid of denitrification, and then when determining that carbon source is added
Between t4；
(6) short-time aeration time t is determined as needed5(taking 7~30min) and sedimentation time t6(taking 40~70min)；
(7) water discharge time t is determined according to the displacement in a cycle7(taking 60~90min)；
(8) at the end of being reacted with sbr reactor device each cycle, the sludge concentration of mixed liquor be 4000~5000mg/L be according to
According to determining the sludge volume of each cycle, and then determine sludge-drainage time t8(taking 5~25min)；
(9) standby time t is determined as needed9(10~50min is taken, is ensureing the processing water of 24 hours 1 day and operation
On the premise of periodicity, t9Value be decided by raw water kelvin nitrogen concentration SoNSituation of change, SoNDuring rise, the cycle of system processing
Time will lengthen, then the standby time t during week9Will accordingly it shorten, on the contrary t9It will extend)；
(10) completed on control device to above-mentioned control parameter δ, n, λ1~λn、τ1~τn、H1~HnAnd t1~t9Value is set
It is fixed；
(11) according to Fig. 1 operational mode, under the domination of control strategy, realize and the On-line Control of processing system is transported
OK.
The basic fundamental process of 2nd step sbr reactor device a cycle operation
(1) water-filling stirring operation starts intake pump, while inlet valve and turn on agitator are opened, by pending original
Water is filled with sbr reactor device and stirs operation.When the first time water-filling water for reaching predetermined (reaches the filling time τ of setting1With
Liquid level H1) when, close inlet valve and water inlet water pump in real time by control system, simultaneously close off agitator.
(2) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and goes water removal
In organic matter, and by ammonium oxidation in water be nitrate nitrogen.In aeration running, according to control strategy, work as on-line monitoring
PH and DO duration curves on characterize characteristic point that nitrification terminates when occurring, air blower and air inlet are closed by control system in real time
Valve, stops aeration operation.
(3) water-filling and stir operation and start intake pump, while water intaking valve and turn on agitator are opened, it is predetermined when reaching
Water-filling water【Reach the filling time τ of settingiWith liquid level Hi(i≥2)】When, close water intaking valve in real time by control system and enter
Water water pump.
In whipping process, denitrifying bacterium is electron donor using the organic matter in water inlet, and denitrification removing upper one is aerobic
Stage produces nitrate nitrogen, while promote denitrification process using the ammonia nitrogen in water inlet, and also removal is certain in denitrification process
Ammonia and nitrogen components.According to control strategy, when the characteristic point that sign denitrification terminates on the pH duration curves of on-line monitoring occurs,
Mixing plant is stopped by control system in real time, stops stirring operation.
(4) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and goes water removal
Middle possible remaining organic matter, and be nitrate nitrogen by ammonium oxidation in water.In aeration running, according to control strategy, when
When the characteristic point that nitrification end is characterized on pH the and DO duration curves of on-line monitoring occurs, air blower is closed by control system in real time
And intake valve, stop aeration operation.
After 2nd stopping aeration operation, system reads water-filling frequency n set in advance automatically, enters if being not reaching to n-1 times
During waterside number, system will return to process (3) and continue water-filling and stir operation；When reaching (n-1)th water inlet number of times, system is entered
Enter to process (5) operation.
(5) n-th water-filling and add carbon source stirring operation intake pump and water intaking valve are opened by control system in real time, to anti-
Device is answered to carry out n-th water-filling, carbon source adds valve and carbon source adds pump and adds carbon source (methanol while being opened in real time by control system
Deng), and start mixing plant.When reaching that filled water amount and carbon source injected volume (reach the filling time τ of settingn, carbon source deliver when
Between t4With liquid level Hn) when, close water intaking valve, water inlet water pump and carbon source in real time by control system and add pump, carbon source and add valve.
In whipping process, denitrifying bacterium is electron donor using the organic matter in n-th water inlet and additional carbon source, instead
Nitrification (n-1)th aerobic stage of removing produces nitrate nitrogen, and the ammonia nitrogen in being intake using n-th promotes denitrification process, while
Ammonia and nitrogen components during n-th is intake are partially removed in denitrification process.According to control strategy, when the pH of on-line monitoring is gone through
When curve on when characterizing the characteristic point that terminates of denitrification and occurring, mixing plant is stopped by control system in real time, stops stirring operation.
(6) short-time aeration operation stops after anoxia stirring, opens air blower and intake valve pair in real time by control system again
Reactor carries out short time blast aeration, and main purpose is the nitrogen that stripping is attached on mud granule and further degraded may
Remaining organic matter and the remaining part ammonia and nitrogen components of oxidation.As the aeration time t for reaching setting5When, it is real-time by control system
Air blower and intake valve are closed, stops aeration operation.
(7) precipitation stops after aeration operation, the mixed liquor in reactor is in precipitated form, realizes mud-water separation.
(8) draining and spoil disposal setting sedimentation time t to be achieved6When, system opens the draining valve on drainage pipeline in real time,
Supernatant after processing is discharged into reactor；According to the spoil disposal scheme of setting, system opens the mud valve on spoil disposal pipeline in real time
Spoil disposal.As the draining t for reaching setting7With sludge-drainage time t8When, system closes draining valve and mud valve in real time.
(9) reactor that leaves unused is in the holding state being stopped, and predetermined standby time t is reached when standby9When, i.e.,
Complete the operation process of SBR technique a cycles.At this moment, system is transferred to next loop cycle operation automatically.
It the composite can be widely applied to the advanced nitrogen processing of nitrogenous organic industrial sewage.
Application example
To simulate nitrogenous organic sewage as process object, to illustrate the application example of the present invention.
Sewage is simulated using soluble starch and sodium acetate as main organic principle, COD value is 630mg/L or so, is used
NH4Cl and KH2PO4Ammonia nitrogen concentration in solution regulation water in N and P concentration, water is 95~109mg/L, and phosphate content expires
Sufficient biological need, using NaHCO3Basicity and pH value are adjusted, makes basicity in water sufficient, pH=7.6~8.0.
Sbr reactor device dischargeable capacity is 12L or so, sets the processing target of denitrogenation as SeN<3mg/L.Take reactor one week
Total water-filling of phase is about 2/3 than δ, use 4 water-fillings (ammonia nitrogen concentration of first time water-filling for 95.5mg/L, rear three water-fillings
Ammonia nitrogen concentration is 107.7mg/L), total filled water amount is 8.2L, and filled water amount 3 times is 2.6L (λ1~λ3It is
31.75%), the 4th filled water amount is 0.4L (λ4=4.88%), the outer carbon source added during the 4th water-filling is methanol.Reactor fills
Sludge concentration after full water is 5000mg/L or so.
The result of the test of the period treatment sewage obtained in the above embodiments is shown in Table 1.
The result of the test of one cycle of 1 sbr reactor device of table, 4 water-filling denitrification processNote
Note：1. during above-mentioned denitrification test, the nitrite nitrogen concentration in each stage of reaction mixed liquor is all approximately
0mg/L, so not being included in nitrite nitrogen parameter in table；
2. the C/N ratios of nitrogenous organic sewage are simulated>5.8, denitrification process carbon source is sufficient, and in each aerobic nitrification knot
COD concentration is equal during beam<30mg/L, the COD concentration of final outflow water<30mg/L, so without row COD parameters in table；
3. aerobic nitrification listed in table terminates the ammonia nitrogen and nitrate nitrogen concentration data in mixed liquor, is aerobic nitrification
During, the respective value when characteristic point that nitrification terminates occurs is indicated on DO and pH duration curves；
4. stirring denitrification listed in table terminates the ammonia nitrogen and nitrate nitrogen concentration data in mixed liquor, is that stirring is anti-
In nitrifying process, the respective value when characteristic point that denitrification terminates occurs is indicated on pH duration curves.
From table 1, in the denitrification process of 4 water-fillings, water outlet total nitrogen is obtained<3mg/L advanced nitrogen effect.Point
Analyse above-mentioned denitrification process to understand, 4 water filling processes, in addition to it can obtain ammonia nitrogen to the beneficial effect of denitrification denitrogenation process,
(see beneficial effects of the present invention) compared with 3 times foregoing water-fillings, more organic matters into water can also be assigned to instead
Nitration section, and then more denitrification additional carbons can be saved and more aerobic process power consumptions are reduced.
3 times foregoing water-fillings, the organic matter for being assigned to denitrification section is 54.6% (see beneficial effects of the present invention).This
During 4 water-fillings of example, the organic matter for being assigned to denitrification section adds up to 68.38% (including in the 2nd time and the 3rd water-filling
Organic matter add up in 63.5%, the 4th water-filling it is organic be 4.88%, 68.38%) both add up to.Consider further that denitrification
During contain appropriate ammonia nitrogen when can save the conclusion more than 10% denitrifying carbon source, during 4 water-fillings, more than 78% depth can be made
Denitrification process is spent without providing outer carbon source.It can be seen that, with the increase of water-filling number of times, the energy-saving effect of denitrification process is also therewith
Enhancing.
Claims (1)
1. a kind of method that batch enters enhanced water SBR technique deep denitrifications, it is characterised in that comprise the following steps：
(1) water-filling stirring operation starts intake pump, while opening inlet valve and turn on agitator, pending raw water is filled
Enter sbr reactor device and stir operation；When reaching predetermined first time water-filling water, inlet valve is closed by control system in real time
With water inlet water pump, agitator is simultaneously closed off；
(2) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and goes in water removal
Organic matter, and be nitrate nitrogen by ammonium oxidation in water；
Start after aeration, real time on-line monitoring pH and DO signal；Monitor the sampling interval t of pH and DO signals on-line1Take 60s；To institute
The pH of collectioniAnd DOiValue carries out the real-time glide filter processing of 4 values, that is, calculates the average value that 4 values are slided, and calculate in real time adjacent
Two glide filter value pHLbi-1、pHLbiWith DOLbi-1、DOLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-
ti-1) and KDOi=(DOLbi-DOLbi-1)/(ti-ti-1) value；In aeration process, when monitoring KpHiIt is worth continuous more than 4min<0
Afterwards, note monitoring KpHiAnd KDOiThe situation of value changes；When monitoring KpHiValue is become just, while meeting K by negativeDOi>KDOi-1>KDOi-2>
KDOi-3>When 0, air blower and intake valve are closed by control system in real time, stop aeration operation；
(3) water-filling stirring operation starts intake pump, while water intaking valve and turn on agitator are opened, water-filling stirring operation；When reaching
During predetermined water-filling water, water intaking valve and water inlet water pump are closed in real time by control system；
Start after stirring, real time on-line monitoring pH signals；Monitor the sampling interval t of pH signals on-line2Take 60s；In whipping process
In, to the pH gatherediValue carries out the real-time glide filter processing of 4 values, that is, calculates the average value that 4 values are slided, and calculate in real time
Two neighboring glide filter value pHLbi-1With pHLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-ti-1)；
In whipping process, when monitoring KpHiIt is worth continuous more than 3min>After 0, note monitoring KpHiThe positive and negative situation of change of value；Work as monitoring
To KpHiValue becomes negative by positive, and keeps t3Time above KpHiValue is equal<When 0, stop stirring operation in real time by control system；t3Take 3~
4min；
(4) aeration operation opens air blower and intake valve in real time by control system, and reactor is aerated and run, and going can in water removal
The remaining organic matter of energy, and be nitrate nitrogen by ammonium oxidation in water；
Start after aeration, real time on-line monitoring pH and DO signal；Monitor the sampling interval t of pH and DO signals on-line1Take 60s；To institute
The pH of collectioniAnd DOiValue carries out the real-time glide filter processing of 4 values, that is, calculates the average value that 4 values are slided, and calculate in real time adjacent
Two glide filter value pHLbi-1、pHLbiWith DOLbi-1、DOLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-
ti-1) and KDOi=(DOLbi-DOLbi-1)/(ti-ti-1) value；In aeration process, when monitoring KpHiIt is worth continuous more than 4min<0
Afterwards, note monitoring KpHiAnd KDOiThe situation of value changes；When monitoring KpHiValue is become just, while meeting K by negativeDOi>KDOi-1>KDOi-2>
KDOi-3>When 0, air blower and intake valve are closed by control system in real time, stop aeration operation；
Stop after aeration operation, system reads water-filling frequency n value set in advance automatically；If the n values read are not reaching to n-1 times
Water-filling number of times, system will return to process (3) and continue water-filling and stir operation；When reaching (n-1)th water-filling number of times, system is entered
Enter to process (5) operation；
(5) n-th water-filling and add carbon source stirring operation intake pump and water intaking valve are opened by control system in real time, to reactor
N-th water-filling is carried out, carbon source adds valve and carbon source adds pump and adds carbon source while being opened in real time by control system, and starts stirring
Device stirring operation；When reaching filled water amount and carbon source injected volume, water intaking valve, water inlet water pump and carbon source are closed in real time by control system
Add pump, carbon source and add valve；
The injected volume of carbon source, according to 4.0<BOD5/ nitrate nitrogen mass concentration<4.2 condition is determined；
Start after stirring, real time on-line monitoring pH signals；Monitor the sampling interval t of pH signals on-line2Take 60s；In whipping process
In, to the pH gatherediValue carries out the real-time glide filter processing of 4 values, that is, calculates the average value that 4 values are slided, and calculate in real time
Two neighboring glide filter value pHLbi-1With pHLbiTo the average rate of change K of timepHi=(pHLbi-pHLbi-1)/(ti-ti-1)；
In whipping process, when monitoring KpHiIt is worth continuous more than 3min>After 0, note monitoring KpHiThe positive and negative situation of change of value；Work as monitoring
To KpHiValue becomes negative by positive, and keeps t3Time above KpHiValue is equal<When 0, stop stirring operation in real time by control system；t3Take 3~
4min；
(6) operation of short time aeration stops after anoxia stirring, opens air blower and intake valve in real time by control system again to anti-
Device is answered to carry out blast aeration, aeration time t5Take 7~30min；As the aeration time t for reaching setting5When, it is real-time by control system
Air blower and intake valve are closed, stops aeration operation；
(7) precipitation stops after short time aeration operation, the mixed liquor in reactor is in precipitated form, carries out mud-water separation；
After mud-water separation, successively through draining, spoil disposal and it is idle after, system is transferred to the circular flow in next cycle；
It is required that BOD in processed raw water5/ total nitrogen>4.0th, total alkalinity/kjeldahl nitrogen>3.6, total alkalinity is with CaCO3Meter, and in raw water
The excursion of kelvin nitrogen concentration is 40~700mg/L, nitrate nitrogen<4mg/L；Above ratio is the ratio between mass concentration；
When processed raw water quality meets above-mentioned condition, the calculation formula of water-filling scheme is as follows：
Work as λn>λ1~(n-1)When, take λn=λ1~(n-1) (2)
N is a cycle total water-filling number of times in formula, and n takes 3~4 times；
λ1~(n-1)The ratio of cycle total filled water amount is accounted for for the 1 to n-1 times filled water amount；
λnThe ratio of cycle total filled water amount is accounted for for n-th filled water amount；
S0NFor the kelvin nitrogen concentration for the raw water that is processed, S0NTake 40~700mg/L；
SeNFor the total nitrogen concentration of water outlet after processing, that is, handle target；
δ is total water-filling ratio in sbr reactor device cycle, and δ takes 1/2~2/3；
Work as λn>λ1~(n-1)When, by λn=λ1~(n-1)(1) formula is brought into obtainThe water-filling ratio of i.e. n times is all
It is equal.
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