CN104986857A - Device and method of combination of denitrification, phosphorous removing and residual sludge fermentation of low-carbon-nitrogen-ratio urban domestic sewage - Google Patents
Device and method of combination of denitrification, phosphorous removing and residual sludge fermentation of low-carbon-nitrogen-ratio urban domestic sewage Download PDFInfo
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Abstract
The invention relates to a device and a method of a combination of denitrification, phosphorous removing and residual sludge fermentation of low-carbon-nitrogen-ratio urban domestic sewage. The invention relates to the technical field of urban domestic sewage treatment. The system comprises a raw water tank, an A/O reactor, a secondary sedimentation tank, an intermediate water tank, a sludge storage tank, a sludge fermentation coupled denitrification and synchronous anaerobic ammonium oxidation autotrophic nitrogen removal sequencing bath reactor (SFDA-SBR), and a computer. The raw water tank is respectively connected with a water inlet end of the A/O reactor and the water inlet end of the SFDA-SBR. A sludge discharge end of the sludge storage tank is connected with a sludge injection end of the SFDA-SBR. According to the method, low-C/N-ratio urban domestic sewage first enters the A/O reactor from the raw water tank, and is subjected to a nitrification reaction and phosphorous removing; water discharged from the A/O reactor enters the intermediate water tank, and enters the SFDA-SBR with residual sludge and low-C/N-ratio urban domestic sewage. With the device and method, deep denitrification can be realized. A needed carbon source is from organics produced by residual sludge fermentation, such that a sludge reduction effect is provided.
Description
Technical field
The present invention relates to the apparatus and method of a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing associating excess sludge fermentation, belong to city domestic sewage biologic treating technique field.First in A/O reactor, realize dephosphorization and nitration reaction, then under the acting in conjunction of acidication bacterium, denitrifying bacteria and anaerobic ammonia oxidizing bacteria, realize the decrement of mud and the efficient removal of sewage total nitrogen in SFDA-SBR.This technology is applicable to the advanced treatment of low C/N ratio (ratio of chemical oxygen demand (COD) mass concentration and total nitrogen concentration) city domestic sewage.
Background technology
In recent years, the excessive eutrophication caused of Water, phosphorus is on the rise, water area ecological environment and human health receive and have a strong impact on, and China is to the effluent quality of municipal sewage plant for this reason, especially stricter to the nitrogen of water outlet, phosphorus index request.Bio-denitrification technology is current most widely used sewage water denitrification technology, and principle is the removal being realized nitrogen by nitrifier and denitrifying bacteria effect, but its key reaching efficient denitrification is sufficient carbon source.
China's major part city domestic sewage, there is the problem of carbon source wretched insufficiency, the carbon source of himself cannot meet the demand of denitrogenation, and then becomes biological sewage treatment total nitrogen key reason not up to standard.Domestic existing sewage biological treatment system carrys out supplementary carbon source demand often through outer carbon sources such as adding methyl alcohol, and this both added processing cost, exacerbates again CO in water factory
2discharge and a large amount of generations of excess sludge.In addition, because the excess sludge production of sewage biological treatment system is large, processing cost is high, for a typical urban sewage treatment system, its sludge treatment cost accounts for greatly 40% of total cost, and the process of excess sludge disposal easily causes the secondary of nutritive element to discharge, and easily causes secondary pollution.
Anaerobic ammonia oxidation process is a kind of bio-denitrifying sewage approach of economical and efficient, its principle is under anoxic conditions, anaerobic ammonia oxidizing bacteria take nitrite nitrogen as electron acceptor(EA), direct is nitrogen by ammonium oxidation, compared with traditional technology, anaerobic ammonia oxidation process is without the need to oxygen supply and organic carbon source, and surplus sludge volume is low, anaerobic ammonia oxidizing bacteria metabolic activity is high, and process volume transformation efficiency is high.But Anammox reaction is matrix with nitrite, usually needs using short distance nitration as pre-treating technology.The realization of short distance nitration generally needs to make nitration reaction only proceed to this step of nitrite nitrogen by restriction dissolved oxygen, free ammonia suppression and hot operation etc., but at the low C/N of process than in the practical application of city domestic sewage, because nitrite accumulation is difficult to remain stable and the sewage warming temperature comparatively condition such as difficulty and being not suitable for economically, short distance nitration is often restricted.
Summary of the invention
In order to solve the problem, the present invention proposes the apparatus and method of a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing associating excess sludge fermentation, nitration reaction and the dephosphorization of sewage is carried out in A/O reactor, carry out the advanced nitrogen of sewage subsequently through external source sludge fermentation, denitrification and Anammox, and mud decrement can be realized simultaneously.
For achieving the above object, the invention provides the device of a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing associating excess sludge fermentation, comprise former pond (1), A/O reactor (2), former water intake pump I (2.1), whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5), second pond (3), secondary clarifier effluent pipe (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), former water intake pump II (6.2), enter dredge pump (6.3), whipping appts II (6.4), computer automatic control system (7), pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2), pH pops one's head in (7.3), ORP pops one's head in (7.4), temperature control heating rod (7.5), temperature monitor and control device (7.6).
Former pond (1) is connected with the feed-water end of A/O reactor (2) and the feed-water end of SFDA-SBR (6) with former water intake pump II (6.2) respectively by former water intake pump I (2.1); Whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5) is provided with in A/O reactor (2); The discharge ends of A/O reactor (2) is connected with the injection side of second pond (3), the draining of second pond (3) flows into intermediate water tank (3) by water shoot (3.1), and the spoil disposal end of second pond (3) is connected with the sludge reflux end of Shou Ge room, A/O reactor (2) anaerobic zone and the note mud end of storage basin (5) with residual sludge pump (3.3) respectively by return sludge pump (3.2); The water side of intermediate water tank (4) is connected with the water injection end of SFDA-SBR (6) by nitrification liquid intake pump (6.1), and the spoil disposal end of storage basin (5) passes through to be connected into the mud inlet end of dredge pump (6.3) with SFDA-SBR (6).SFDA-SBR (6) inside arranges pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), be connected with pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) respectively, controller is connected with computer automatic control system (7).
A/O reactor (1) dividing plate of the water hole that is crisscross arranged up and down is divided into 6-9 lattice room, be provided with the lattice room, anaerobic zone and lattice room, aerobic zone that are connected according to this, lattice room, anaerobic zone is divided into 2-3 lattice room, be provided with whipping appts I (2.2), lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head (2.3), provide air by air compressor (2.4).
SFDA-SBR (6) inside arranges whipping appts II (6.4), pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), and probe is connected with computer automatic control system (7) with temperature monitor and control device (7.6) respectively by pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) with heating rod.Computer automatic control system (7) by Online Monitoring Control device by SFDA-SBR internal temperature control at 30 ± 1 DEG C, wherein pH, the ORP of any instant, Temperature displaying on computer display screen, and can draw pH, ORP change in process curve automatically.
The present invention provides a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing to combine the method for excess sludge fermentation simultaneously, comprises the following steps:
(1) A/O reactor is started: with the sludge from final clarifier of municipal sewage plant for seed sludge injects A/O reactor, its sludge concentration is 2000-4000mg/L, meanwhile, inject former pond than city domestic sewage as former water using low C/N, squeeze in A/O reactor by former water intake pump I; Start stirring system and aerating system subsequently, phosphorus reaction is put in lattice room, A/O reactor anaerobic zone, there is nitrated suction phosphorus reaction in lattice room, aerobic zone, in reaction process, DO maintains 2-3mg/L, flooding velocity is regulated to make the hydraulic detention time of Mei Ge room, A/O reactor anaerobic zone be 0.5h ~ 1.0h, the hydraulic detention time of Mei Ge room, aerobic zone is 1.0h ~ 2.0h, the hydraulic detention time of second pond is 1.0h ~ 1.5h, open sludge reflux pump and residual sludge pump, conditioning of mud reflux ratio is 50% ~ 100%.
(2) startup starting SFDA-SBR:SFDA-SBR is divided into three phases, stage one, / the mud of anoxic sludge system is detested in inoculation, its sludge concentration is 3000 ~ 4000mg/L, SFDA-SBR is added as former water using the mixing solutions of sodium acetate, SODIUMNITRATE, in mixed solution, the mass ratio of carbon element and nitrogen is 2 ~ 3, stir under anoxic conditions, to observe in reactor that pH constantly slows down rising, ORP constantly slows down decline, but ORP value is greater than-300mV all the time, steady running reaches more than 80% to nitrous accumulation rate, and the domestication achieving part denitrification mud is cultivated; In the stage two, reduce the amount of sodium acetate in water inlet, replace the sodium acetate reduced with excess sludge of municipal sewage plant, increase the input amount of excess sludge, until sodium acetate is all substituted by excess sludge.Using voltaile fatty acid (VFAs) the substituted acetic acid sodium of excess sludge fermentation generation as denitrifying carbon source.It is 8.0 ~ 9.0 that hydrogen injecting sodium hydroxide solution controls pH in reactor, and maintaining reactor temperature by heating rod is 30 DEG C, realizes the coupling of denitrification and excess sludge fermentation.Replace sodium nitrate solution as water inlet with the nitrification liquid of A/O reactor water outlet, make final nitrous accumulation rate still reach more than 80%; In the stage three, sludge concentration in reactor is made to be 5000 ~ 6000mg/L to the anaerobic ammonium oxidation sludge inoculating steady running more than ten months during denitrification and excess sludge ferment the SFDA-SBR that is coupled.To low C/N than the water outlet nitrification liquid adding A/O reactor in sanitary sewage, the mass ratio of ammonia nitrogen and nitric nitrogen is made to be 1:1.5 ~ 1:10, SFDA-SBR is injected in this, as water inlet, when TN clearance in SFDA-SBR when continuing maintenance more than 15 days, reaches the realization of excess sludge fermentation coupling denitrification synchronous anaerobic ammonia oxidation autotrophic denitrification higher than 90%.
(3) series operation A/O reactor and SFDA-SBR: the low C/N in raw water box squeezes into A/O reactor than sanitary sewage by former water intake pump I, sludge concentration is 2000-3000mg/L, start whipping appts I subsequently, adjusting gas flow meter makes dissolved oxygen maintain 2-3mg/L, the water outlet of A/O reactor enters second pond, after mud-water separation, precipitating sludge is back to the sludge reflux end of the Shou Ge room, anaerobic zone of A/O reactor, control of reflux ratio is at 50%-100%, supernatant liquor flows into intermediate water tank by rising pipe, open two intake pumps connecting SFDA-SBR, regulate pump speed, former water volume and nitrification liquid volume ratio of intaking of intaking is made to be 1:1.5 ~ 1:10, total water inlet volume is 3/5 ~ 4/5 of SFDA-SBR useful volume, simultaneously, fresh excess sludge in storage basin passes through to inject SFDA-SBR into dredge pump, regulate pump speed, enter the 1/5-2/5 that mud volume is SFDA-SBR useful volume, intake into mud time 0.5h, anoxia stirring 4.5h, precipitation 1h, draining 0.25h, draining ratio is 0.5 ~ 0.7, run 1-2 cycle every day.
Know-why of the present invention is as follows:
First low C/N enters A/O reactor than city domestic sewage, in anaerobic zone, polyP bacteria under anaerobic, polyphosphoric acid salt in decomposer produces ATP, utilize ATP to absorb sewage mesostroma in active transport mode to enter in cell and synthesize PHB, discharge phosphoric acid salt in environment simultaneously, be called for short anaerobic phosphorus release reaction, then aerobic zone is entered, polyP bacteria is under aerobic condition, decompose the PHB in body and Exogenous ground substance, external phosphoric acid salt is transported in body and synthesizes ATP and nucleic acid by generation proton motive force, the phosphoric acid salt of surplus is aggregated into storage of cells thing, be called for short aerobic suction phosphorus reaction, simultaneously under aerobic condition, under the effect of nitrococcus and nitrifier, be nitrite nitrogen by the ammonia nitrogen initial oxidation in sewage, then reoxidize as nitric nitrogen, be called for short nitration reaction, nitrification liquid enters SFDA-SBR, in the reactor on the one hand, the nitric nitrogen part denitrification produced in nitric nitrogen in nitrification liquid and anaerobic ammonium oxidation process is nitrite nitrogen by the carbon source that denitrifying bacteria can utilize excess sludge fermentation to produce, and nitric nitrogen remaining in system and nitrite nitrogen can also be reduced to nitrogen and remove from system, on the other hand, utilize the autotrophic denitrification ability of anaerobic ammonia oxidizing bacteria, the nitrous that the ammonia nitrogen produced from the ammonia nitrogen in former water and excess sludge fermentation and part denitrification produce is converted into nitrogen remove from system, thus realize the advanced nitrogen of whole system, make excess sludge be utilized effectively simultaneously, realize mud decrement.Key of the present invention is, part denitrifying bacteria is tamed out by matching well Aquaponic with low C/N, make nitrous accumulation rate stable maintenance more than 80%, thus guarantee that in excess sludge fermentation coupling unit denitrification synchronous anaerobic ammonia oxidation autotrophic denitrification system, anaerobic ammonia oxidizing bacteria has enough substrates.
Compared with prior art, the present invention has the following advantages:
1, by being fermented by excess sludge, denitrification and Anammox autotrophic denitrification organically combine, and realize low C/N than the advanced nitrogen of city domestic sewage and excess sludge reduction, reach to save sewage water denitrification carbon source and add the object with processing cost;
2, because microbial population in excess sludge fermentation coupling denitrification synchronous anaerobic ammonia oxidation self-supported denitrification reactor has diversity, even if city domestic sewage once in a while variation water quality is very large, still can realize the efficient removal of total nitrogen, namely this system can successfully manage nitrogen load impact;
3, realize the minimizing disposal and utilization of bio-denitrifying sewage system self residual mud, improve mud and sewage processing efficiency, save processing cost and floor space.
4, whole technological operation is simple, and only need set flooding velocity and the reaction times in SFDA-SBR each stage of two reactors, without the need to the control process of complexity, water outlet TN can meet emission standard.
Accompanying drawing explanation
Fig. 1 is the structure iron of apparatus of the present invention.
Primary symbols is described as follows:
1-former pond 2-A/O reactor 3-second pond
4-intermediate water tank 5-storage basin
6-excess sludge fermentation coupling denitrification synchronous anaerobic ammonia oxidation autotrophic denitrification SBR
2.1-former water intake pump 2.2-whipping appts I 2.3-aeration head
2.4-air compressor 2.5-gas meter 3.1-nitrification liquid rising pipe
3.2-sludge reflux pump 3.3-residual sludge pump 6.1-nitrification liquid intake pump
6.2-former water intake pump 6.3-enters dredge pump 6.4-whipping appts II
7.1-pH process Online Monitoring Control device 7.2-ORP process Online Monitoring Control device
7.3-pH probe 7.4-ORP probe 7.5-temperature control heating rod
7.6-on-line temperature monitoring controller
Embodiment
In conjunction with the accompanying drawings and embodiments the present invention is described in further detail.
As shown in Figure 1, the device of a kind of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing associating excess sludge fermentation, comprise former pond (1), A/O reactor (2), former water intake pump I (2.1), whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5), second pond (3), secondary clarifier effluent pipe (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), former water intake pump II (6.2), enter dredge pump (6.3), whipping appts II (6.4), computer automatic control system (7), pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2), pH pops one's head in (7.3), ORP pops one's head in (7.4), temperature control heating rod (7.5), temperature monitor and control device (7.6).
Former pond (1) is connected with the feed-water end of A/O reactor (2) and the feed-water end of SFDA-SBR (6) with former water intake pump II (6.2) respectively by former water intake pump I (2.1); Whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5) is provided with in A/O reactor (2); The discharge ends of A/O reactor (2) is connected with the injection side of second pond (3), the draining of second pond (3) flows into intermediate water tank (3) by water shoot (3.1), and the spoil disposal end of second pond (3) is connected with the sludge reflux end of Shou Ge room, A/O reactor (2) anaerobic zone and the note mud end of storage basin (5) with residual sludge pump (3.3) respectively by return sludge pump (3.2); The water side of intermediate water tank (4) is connected with the water injection end of SFDA-SBR (6) by nitrification liquid intake pump (6.1), and the spoil disposal end of storage basin (5) passes through to be connected into the mud inlet end of dredge pump (6.3) with SFDA-SBR (6).SFDA-SBR (6) inside arranges pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), be connected with pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) respectively, controller is connected with computer automatic control system (7).
A/O reactor (1) dividing plate of the water hole that is crisscross arranged up and down is divided into 6-9 lattice room, be provided with the lattice room, anaerobic zone and lattice room, aerobic zone that are connected according to this, lattice room, anaerobic zone is divided into 2-3 lattice room, be provided with whipping appts I (2.2), lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head (2.3), provide air by air compressor (2.4).
SFDA-SBR (6) inside arranges whipping appts II (6.4), pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), and probe is connected with computer automatic control system (7) with temperature monitor and control device (7.6) respectively by pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) with heating rod.Computer automatic control system (7) by Online Monitoring Control device by SFDA-SBR internal temperature control at 30 DEG C, wherein pH, the ORP of any instant, Temperature displaying on computer display screen, and can draw pH, ORP change in process curve automatically.
Specific experiment case is as follows:
Concrete test water adopts Beijing University of Technology's dependents' district sanitary sewage as former water, and concrete water quality is as follows: COD concentration is 180-300mg/L, NH
4 +-N concentration is 50-85mg/L, NO
2 --N and NO
3 --N is all below detectability, and COD/N ratio is 2.2 ~ 3.5, belongs to typical low C/N and compares sewage.A/O reactor useful volume used is 9L, is divided into 6 lattice rooms, and front two lattice rooms are anaerobic zone, rear four lattice rooms are aerobic zone, and the water flowing duct staggered up and down that each lattice room is arranged on each dividing plate along water (flow) direction connects, and its total hrt is 8h, wherein the anaerobism time is 2h, and aerobic time is 6h.The useful volume of SFDA-SBR used is 10L, and draining ratio is 0.6, runs 2 cycles every day, and each cycle comprises into water 0.5h, stirs 4.5h, precipitation 1.0h, draining 0.25h.Carrying out practically process is as follows:
(1) in former pond and storage basin, low C/N is filled respectively than the fresh excess sludge of city domestic sewage and municipal sewage plant.
(2) A/O reactor carries out nitrification and phosphorus removal process: A/O reactor seed sludge is municipal sewage plant's sludge from final clarifier, there is good denitrogenation dephosphorizing ability, the low C/N injected in seed sludge and former pond is mixed to form the mixed solution of 2500mg/L than city domestic sewage, injects A/O reactor and second pond.Open whipping appts, the air compressor in A/O reactor, adjusting gas flow meter, controls the DO concentration in A/O reactor between 2 ~ 3mg/L.Opening A/O intake pump starts injecting low C/N in A/O reactor than city domestic sewage, and start sludge reflux pump and residual sludge pump, return sludge ratio is 60% simultaneously, starts the nitrification and phosphorus removal treating processes of A/O reactor.
(3) in nitrification and phosphorus removal treating processes, maintain the ammonia oxidation rate of A/O water outlet more than 85%, wherein NO3-N accumulation rate is greater than 90%, and regulates the dissolved oxygen concentration of aerobic zone in A/O reactor with this, and the SRT simultaneously maintaining A/O treatment system is about 30d.
(4) after treating to fill the nitrification liquid from the discharge of A/O reactor in intermediate water tank, open two intake pumps connecting SFDA-SBR, regulate pump speed, former water volume and nitrification liquid volume ratio of intaking of intaking is made to be 1:6, total water inlet volume is 4/5 of SFDA-SBR useful volume, simultaneously, fresh excess sludge in storage basin passes through to inject SFDA-SBR into dredge pump, regulates pump speed, enter that mud volume is SFDA-SBR useful volume 1/5, intake into mud time 0.5h, anoxia stirring 4.5h, precipitation 1h, draining 0.25h, draining ratio is 0.6, runs 2 cycles every day.
Before system is run continuously, first SFDA-SBR is started, detailed process is divided into the next stage: the stage one, / the mud of anoxic sludge system is detested in inoculation, its sludge concentration is 3000 ~ 4000mg/L, with sodium acetate, the mixing solutions of SODIUMNITRATE adds SFDA-SBR as former water, in mixed solution, the mass ratio of carbon element and nitrogen is 2 ~ 3, stir under anoxic conditions, to observe in reactor that pH constantly slows down rising, ORP constantly slows down decline, but ORP value is greater than-300mV all the time, steady running reaches more than 80% to sub-accumulation rate, the domestication achieving part denitrification mud is cultivated, in the stage two, reduce the amount of sodium acetate in water inlet, replace the sodium acetate reduced with excess sludge of municipal sewage plant, increase the input amount of excess sludge, until sodium acetate is all replaced by excess sludge.Using the voltaile fatty acid substituted acetic acid sodium of excess sludge fermentation generation as denitrifying carbon source.It is 8.0 ~ 9.0 that hydrogen injecting sodium hydroxide solution controls pH in reactor, and maintaining reactor temperature by heating rod is 30 DEG C, realizes the coupling of denitrification and excess sludge fermentation.Replace sodium nitrate solution as water inlet with the nitrification liquid of A/O reactor water outlet, make final nitrous accumulation rate still reach more than 80%; In the stage three, sludge concentration in reactor is made to be 5000 ~ 6000mg/L to the anaerobic ammonium oxidation sludge inoculating steady running more than ten months during denitrification and excess sludge ferment the SFDA-SBR that is coupled.To low C/N than add in sanitary sewage A/O reactor water outlet nitrification liquid, the mass ratio of ammonia nitrogen and nitric nitrogen is made to be 1:1.5 ~ 1:10, using this mixed solution as the water inlet of SFDA-SBR, when TN clearance in SFDA-SBR when continuing maintenance more than 15 days, reaches the realization of excess sludge fermentation coupling denitrification synchronous anaerobic ammonia oxidation autotrophic denitrification higher than 90%.
The excess sludge low C/N of synchronous advanced treatment that ferments compares city domestic sewage than the low C/N of the device process of city domestic 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, simultaneously mud decrement about 30%.
Claims (2)
1. the treatment unit of low ratio of carbon to ammonium city domestic sewage denitrogenation dephosphorizing associating excess sludge fermentation, it is characterized in that: comprise former pond (1), A/O reactor (2), former water intake pump I (2.1), whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5), second pond (3), secondary clarifier effluent pipe (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), former water intake pump II (6.2), enter dredge pump (6.3), whipping appts II (6.4), computer automatic control system (7), pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2), pH pops one's head in (7.3), ORP pops one's head in (7.4), temperature control heating rod (7.5), temperature monitor and control device (7.6),
Former pond (1) is connected with the feed-water end of A/O reactor (2) and the feed-water end of SFDA-SBR (6) with former water intake pump II (6.2) respectively by former water intake pump I (2.1); Whipping appts I (2.2), aeration head (2.3), air compressor (2.4), gas meter (2.5) is provided with in A/O reactor (2); The discharge ends of A/O reactor (2) is connected with the injection side of second pond (3), the draining of second pond (3) flows into intermediate water tank (3) by water shoot (3.1), and the spoil disposal end of second pond (3) is connected with the sludge reflux end of Shou Ge room, A/O reactor (2) anaerobic zone and the note mud end of storage basin (5) with residual sludge pump (3.3) respectively by return sludge pump (3.2); The water side of intermediate water tank (4) is connected with the water injection end of SFDA-SBR (6) by nitrification liquid intake pump (6.1), and the spoil disposal end of storage basin (5) passes through to be connected into the mud inlet end of dredge pump (6.3) with SFDA-SBR (6); SFDA-SBR (6) inside arranges pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), be connected with pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) and temperature monitor and control device (7.6) respectively, controller is connected with computer automatic control system (7);
A/O reactor (1) dividing plate of the water hole that is crisscross arranged up and down is divided into 6-9 lattice room, be provided with the lattice room, anaerobic zone and lattice room, aerobic zone that are connected according to this, lattice room, anaerobic zone is divided into 2-3 lattice room, be provided with whipping appts I (2.2), lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head (2.3), provide air by air compressor (2.4);
SFDA-SBR (6) inside arranges whipping appts II (6.4), pH probe (7.3), ORP pops one's head in (7.4) and temperature control heating rod (7.5), and probe is connected with computer automatic control system (7) with temperature monitor and control device (7.6) respectively by pH process Online Monitoring Control device (7.1), ORP process Online Monitoring Control device (7.2) with heating rod; Computer automatic control system (7) by Online Monitoring Control device by SFDA-SBR internal temperature control at 30 ± 1 DEG C, wherein pH, the ORP of any instant, Temperature displaying on computer display screen, and can draw pH, ORP change in process curve automatically.
2. application rights requires the method for device described in 1, it is characterized in that, comprises the following steps:
(1) A/O reactor is started: with the sludge from final clarifier of municipal sewage plant for seed sludge injects A/O reactor, its sludge concentration is 2000-4000mg/L, meanwhile, inject former pond than city domestic sewage as former water using low C/N, squeeze in A/O reactor by former water intake pump I; Start stirring system and aerating system subsequently, phosphorus reaction is put in lattice room, A/O reactor anaerobic zone, there is nitrated suction phosphorus reaction in lattice room, aerobic zone, in reaction process, DO maintains 2-3mg/L, flooding velocity is regulated to make the hydraulic detention time of Mei Ge room, A/O reactor anaerobic zone be 0.5h ~ 1.0h, the hydraulic detention time of Mei Ge room, aerobic zone is 1.0h ~ 2.0h, the hydraulic detention time of second pond is 1.0h ~ 1.5h, open sludge reflux pump and residual sludge pump, conditioning of mud reflux ratio is 50% ~ 100%;
(2) starting the startup of SFDA-SBR:SFDA-SBR and be divided into three phases, the stage one, inoculation detests/mud of anoxic sludge system, its sludge concentration is 3000 ~ 4000mg/L; SFDA-SBR is added as former water using the mixing solutions of sodium acetate, SODIUMNITRATE, in mixed solution, the mass ratio of carbon element and nitrogen is 2 ~ 3, stir under anoxic conditions, to observe in reactor that pH constantly slows down rising, ORP constantly slows down decline, but ORP value is greater than-300mV all the time, steady running reaches more than 80% to nitrous accumulation rate, and the domestication achieving part denitrification mud is cultivated; In the stage two, reduce the amount of sodium acetate in water inlet, replace the sodium acetate reduced with excess sludge of municipal sewage plant, increase the input amount of excess sludge, until sodium acetate is all substituted by excess sludge; Using the voltaile fatty acid substituted acetic acid sodium of excess sludge fermentation generation as denitrifying carbon source; It is 8.0 ~ 9.0 that hydrogen injecting sodium hydroxide solution controls pH in reactor, and maintaining reactor temperature by heating rod is 30 DEG C, realizes the coupling of denitrification and excess sludge fermentation; Replace sodium nitrate solution as water inlet with the nitrification liquid of A/O reactor water outlet, make final nitrous accumulation rate still reach more than 80%; In the stage three, sludge concentration in reactor is made to be 5000 ~ 6000mg/L to the anaerobic ammonium oxidation sludge inoculating steady running more than ten months during denitrification and excess sludge ferment the SFDA-SBR that is coupled; To low C/N than the water outlet nitrification liquid adding A/O reactor in sanitary sewage, the mass ratio of ammonia nitrogen and nitric nitrogen is made to be 1:1.5 ~ 1:10, SFDA-SBR is injected in this, as water inlet, when TN clearance in SFDA-SBR when continuing maintenance more than 15 days, reaches the realization of excess sludge fermentation coupling denitrification synchronous anaerobic ammonia oxidation autotrophic denitrification higher than 90%;
(3) series operation A/O reactor and SFDA-SBR: the low C/N in raw water box squeezes into A/O reactor than sanitary sewage by former water intake pump I, sludge concentration is 2000-3000mg/L, start whipping appts I subsequently, adjusting gas flow meter makes dissolved oxygen maintain 2-3mg/L, the water outlet of A/O reactor enters second pond, after mud-water separation, precipitating sludge is back to the sludge reflux end of the Shou Ge room, anaerobic zone of A/O reactor, control of reflux ratio is at 50%-100%, supernatant liquor flows into intermediate water tank by rising pipe, open two intake pumps connecting SFDA-SBR, regulate pump speed, former water volume and nitrification liquid volume ratio of intaking of intaking is made to be 1:1.5 ~ 1:10, total water inlet volume is 3/5 ~ 4/5 of SFDA-SBR useful volume, simultaneously, fresh excess sludge in storage basin passes through to inject SFDA-SBR into dredge pump, regulate pump speed, enter the 1/5-2/5 that mud volume is SFDA-SBR useful volume, intake into mud time 0.5h, anoxia stirring 4.5h, precipitation 1h, draining 0.25h, draining ratio is 0.5 ~ 0.7, run 1-2 cycle every day.
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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 |
| CN110002592A (en) * | 2019-05-05 | 2019-07-12 | 北京工业大学 | Short-cut denitrification-sludge fermentation coupling Anaerobic ammonium oxidation system processing sanitary sewage device and method |
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