CN103693813B - Device and method for strengthening sludge digestion and synchronously denitrifying and dephosphorizing - Google Patents
Device and method for strengthening sludge digestion and synchronously denitrifying and dephosphorizing Download PDFInfo
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Abstract
The invention relates to a device and a method for strengthening sludge digestion and synchronously denitrifying and dephosphorizing, and belongs to the technical field of low-carbon-nitrogen-ratio (C/N) and high-concentration ammonia nitrogen wastewater biological denitrification. The device is provided with a raw water tank, an A-O (anaerobic-oxic) reactor, a sedimentation tank, a sludge fermentation, coupling and denitrification synchronization autotrophic denitrification (SFDANR) reactor and a sludge storage tank, wherein the raw water tank is connected with the A-O reactor by a raw water inlet pump; a water outlet of the sedimentation tank is connected with the SFDANR reactor by a water outlet pump; and the SFDANR reactor is provided with a self-circulation pipeline. The method comprises the following steps of starting the A-O reactor, starting the SFDANR reactor, and allowing the A-O reactor and the SFDANR reactor to run in series. The device and the method are suitable for deep denitrification and dephosphorization of high ammonia nitrogen domestic sewage and a sludge digestion solution; a technology is advanced; a sludge yield is reduced effectively; and energy saving and consumption reduction advantages are obvious.
Description
Technical field
The present invention relates to the digestion of a kind of reinforcement sludge and the apparatus and method of synchronous denitrification dephosphorizing, belong to biochemical process Sewage Sludge Treatment Techniques field.The ammonia nitrogen of sludge fermentation release and short distance nitration are reacted the nitrous produced and are removed by Anammox, the nitric nitrogen denitrification produced is removed as electron donor by the VFA that denitrifying bacteria utilizes acidication to produce, and reaches the degree of depth removal of total nitrogen and effective utilization of mud.This technology is applicable to low C/N ratio, C/P is than the intensified denitrification and dephosphorization of sewage and the preliminary decrement of mud and stablize.
Background technology
" urban wastewater treatment firm pollutant emission standard " (GB18918-2002) middle one-level A standard-required pollutant discharging unit effluent quality that China promulgated in 2002 is that COD is less than 50mg/L, and ammonia nitrogen is less than 5mg/L, and total nitrogen is less than 15mg/L, and total phosphorus is less than 0.5mg/L.Domestic many Sewage Plant can not realize the qualified discharge of total nitrogen, how to improve traditional technology denitrification effect, are the active demands of present stage field of municipal sewage treatment.
Municipal effluent C/N is more on the low side than generally in China, cannot meet the demand of denitrogenation, and carbon source deficiency becomes municipal sewage treatment key reason not up to standard, for solving this problem, has the organism of research and utilization excess sludge fermentation generation at present as denitrification and carbon source.Traditional sludge fermentation and carbon source extractive technique are generally fermentation--eluriate technique, namely mud acidication in fermentor tank produces voltaile fatty acid etc. and can utilize organism, utilize water inlet to eluriate subsequently, then elutriation liquid is squeezed into bio-reaction zone in order to strengthen Nitrogen/Phosphorus Removal.Utilize fermentation--eluriate technique and there is following shortcoming in actual applications: due to the adsorption of mud, mud-water separation difficulty, the VFA that fermentation produces is difficult to be eluriated out and wants higher elutriation efficiency and then needs the larger elutriation water yield; In complete anaerobic reactor, be difficult to avoid methane phase to react occur, and particulate matter hydrolysis is the rate-limiting step of sludge anaerobic fermentation, therefore tunning is consumed in a large number by methanogen; Then needing larger elutriation water consumption for reaching higher elutriation efficiency, certainly leading to larger upflow velocity, taking a lot of particulate matter out of, and then increase the solid loading of subsequent processing units.
Excess sludge fermentation coupling denitrification strengthening sewage denitrification is that a kind of novel carbon source develops technique, and tool has the following advantages: 1) due to NO
x -the existence of-N, avoids the generation of methane phase reaction, prevents tunning to be consumed by methanogen; 2) VFA is utilized by the denitrifying bacteria of surrounding after producing immediately, reduces substrate feedback inhibition, stimulates carrying out further of sludge fermentation; 3) anti-nitration reaction produces basicity, runs, carry out pH and rise gradually, avoid system acidifying problem in normal fermentation with denitrification under reactor can be made to remain on the condition of neutrality and meta-alkalescence; 4) omit the panning procedure in traditional technology, run simple to operation, replicability is strong.
Summary of the invention
The object of this invention is to provide a kind of make high ammonia-nitrogen wastewater advanced nitrogen while, the apparatus and method that mud effectively utilizes can also be realized.
For achieving the above object, the invention provides the digestion of a kind of reinforcement sludge and the device of synchronous denitrification dephosphorizing, comprise raw water box 1, former water intake pump 1.1, A-O reactor 2, whipping appts 2.1, air compressor 2.2, aeration head 2.3, settling tank 2.4, sludge reflux pump 2.5, mud valve 2.6, go out water pump 2.7, SFDANR reactor 3, intermediate water tank 3.1, recycle pump 3.2, circulation control valve 3.3, exhaust-valve 3.4, gas extractor 3.5, sealing plate 3.6, cylindrical sludge bed 3.7, water-distributing device 3.8, triphase separator 3.9, heating zone device 3.10, rising pipe 3.11, sponge filler 3.12, water distributing pore 3.13, storage basin 4, enter dredge pump 4.1.
Raw water box 1 is connected with A-O reactor 2 by former water intake pump 1.1, A-O reactor 2 is connected with settling tank 2.4 by rising pipe, be connected with the first lattice room of A-O reactor 2 by sludge reflux pump 2.5 bottom settling tank 2.4, settling tank 2.4 passes through water pump 2.7 and is connected with bottom SFDANR reactor 3, and storage basin 4 passes through to be connected into dredge pump 4.1 with bottom mud SFDANR reactor 3.
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 2.1, lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head 2.3, provide pressure by air compressor 2.2.
SFDANR reactor 3 is provided with cylindrical sludge bed 3.7, and top is provided with top sealing plate 3.6 and triphase separator 3.9, and centre is provided with temperature control heating belting 3.10, and bottom is provided with water-distributing device 3.8; Triphase separator 3.9 is connected with gas extractor 3.5 by pipeline; Cylindrical sludge bed 3.7 top is connected with bottom SFDANR reactor 3 with circulation control valve 3.2 by intermediate water tank 3.1, recycle pump 3.2; SFDANR reactor 3 water outlet is discharged by rising pipe 3.11.
The present invention provides reinforcement sludge to digest and the method for synchronous denitrification dephosphorizing simultaneously, comprises the following steps: comprise the following steps:
(1) A-O reactor is started: with the anaerobic-aerobic disposal mud of actual cities sewage work for inoculation mud injects A-O reactor, sludge concentration is 2000-3000mg/L, hydraulic detention time 5-8h, sludge retention time 15-25 days; NH will be added
4hCO
3actual cities sanitary sewage pump into lattice room, A-O reactor anaerobic zone, start whipping appts subsequently, regulate aerating system flow to make dissolved oxygen maintain 1.5-2.5mg/L, control to add NH
4hCO
3concentration make influent ammonia nitrogen loading maintain 0.2-0.3kgNH
4 +-N/m
3d, pH value controls at 8.0-9.0, and water outlet enters settling tank, and precipitating sludge is back to the first lattice room of A-O reactor, and control of reflux ratio is at 50%-100%.Run A-O reactor under these conditions, when water outlet phosphate concn lower than 0.5mg/L and accumulation rate of nitrite be greater than 90% continue maintenance 15 days time, dephosphorization process and short distance nitration are achieved.
(2) start SFDANR reactor: sludge concentration 7000-8000mg/L in control SFDANR reactor, hydraulic detention time 3-5h, sludge retention time 10-20 days, water inlet adopts NH
4 +-N and NO
2 --N mass ratio is the artificial distribution of 1:1.3, initial TN concentration is 20mg/L and progressively increases nitrogen load until 200mg/L with the gradient of 20mg/L, the end time of each increase nitrogen load is that autotrophic denitrification rate continues maintenance more than 15 days more than 95%, finally completes the Anammox acclimation to SFDANR reactor; Water inlet adopts NH
4 +-N and NO
2 --N mass ratio is 1:1.3 and TN is the artificial distribution of 200mg/L, add sodium acetate makes SCOD concentration be 100-150mg/L as denitrifying carbon source simultaneously, when TN clearance higher than 90% and continue maintenance more than 15 days time, Anammox and denitrifying coupling successfully realize; Make SCOD concentration continue to maintain 100-150mg/L using excess sludge substituted acetic acid sodium as denitrifying carbon source, when TN clearance higher than 90% and continue maintenance more than 15 days time, reach autotrophic denitrification synchronous sludge fermentation coupling denitrification realization.
(3) after A-O reactor and SFDANR reactor complete startup respectively, by whole device series operation: the high ammonia-nitrogen wastewater in raw water box squeezes into A-O reactor by former water intake pump, sludge concentration is 2000-3000mg/L, hydraulic detention time 5-8h, sludge retention time 15-25 days, start whipping appts subsequently, regulate aerating system flow to make dissolved oxygen maintain 1.5-2.5mg/L, pH value controls at 8.0-9.0, the water outlet of A-O reactor enters settling tank, after mud-water separation, precipitating sludge is back to the first lattice room of A-O reactor, control of reflux ratio is at 50%-100%, supernatant liquor enters SFDANR reactor by water outlet infusion, simultaneously, fresh excess sludge in storage basin passes through to inject SFDANR reactor into dredge pump, sludge concentration 7000-8000mg/L in control SFDANR reactor, hydraulic detention time 3-5h, sludge retention time 10-20 days, self-circulation reflux ratio 80%-150%, finally realize excess sludge and nitrification liquid ferments at SFDANR reactor, the coupling processing of denitrification and Anammox, water outlet after process and mud are respectively by water shoot and mud valve, exhaust-valve discharges.
Know-why of the present invention is as follows:
First high ammonia-nitrogen wastewater enters A-O reactor, controls sludge retention time on the one hand, and then realize the removal of phosphorus in former water by spoil disposal, is realized the short distance nitration of waste water on the other hand by aeration control; Nitrification liquid enters SFDANR reactor, utilize the autotrophic denitrification ability of anaerobic ammonia oxidizing bacteria on the one hand, by from the ammonia nitrogen removal discharged in the nitrous of A-O reactor and sludge fermentation process, on the other hand, the carbon source that denitrifying bacteria utilizes sludge fermentation to produce, is reduced into nitrogen by the nitre nitrogen that anaerobic ammonium oxidation process and A-O reactor nitrifying process produce, thus realizes the advanced nitrogen of whole system, make excess sludge obtain effective utilization simultaneously, promote mud decrement.Key of the present invention is, by aeration regulation and control in A-O reactor, ensures that nitrous has sufficient accumulation rate, thus guarantees that in the synchronous autotrophic denitrification system of sludge fermentation coupling denitrification, anaerobic ammonia oxidizing bacteria has significant proportion to exist.
Compared with prior art, the present invention has the following advantages:
1. denitrification effect is stablized.This device can be resisted certain ammonia nitrogen and impact, even if A-O reactor can not play short distance nitration effectiveness completely, nitric nitrogen still can be removed by denitrification by the synchronous self-supported denitrification reactor of sludge fermentation coupling denitrification.
2. phosphor-removing effect is good.PolyP bacteria makes full use of organism limited in former water to carry out releasing phosphorus as carbon source, then carries out suction phosphorus at aerobic stage, enhances the removal effect of whole process total phosphorus.
3. fermentation rate is high.In the process of sludge fermentation coupling denitrification, tunning is consumed in a large number by denitrification flora, reduces substrate inhibition, and fermentation rate and traditional sludge are fermented and eluriated compared with technique and will improve further.
4. sludge yield is few.Whole device only has dephosphorization and sludge fermentation process to create excess sludge, and bio-denitrifying sewage system self residual mud achieves minimizing process and effectively utilizes, and reduces sewage plant sludge processing costs.
Accompanying drawing explanation
Fig. 1 is the structural representation of apparatus of the present invention
Fig. 2 is SFDANR inside reactor structural representation
Fig. 3 is water-distributing device orthographic plan
Primary symbols is described as follows:
1-former pond 2-A-O reactor
The former water intake pump of 3-SFDANR reactor 4-storage basin 1.1-
2.1-whipping appts 2.2-air compressor 2.3-aeration head
2.4-settling tank 2.5-sludge reflux pump 2.6-mud valve
2.7-goes out water pump 3.1-intermediate water tank 3.2-recycle pump
3.3-circulation control valve 3.4-exhaust-valve 3.5-gas extractor
3.6-sealing plate 3.7-cylindrical sludge bed 3.8-water-distributing device
3.9-triphase separator 3.10-heating zone device 3.11-rising pipe
3.12-sponge filler 3.13-water distributing pore 4.1-enters dredge pump
Embodiment
In conjunction with the accompanying drawings and embodiments the present invention is described in further detail.
As Fig. 1, Fig. 2, shown in Fig. 3, reinforcement sludge digests and the device of synchronous denitrification dephosphorizing, comprise raw water box 1, former water intake pump 1.1, A-O reactor 2, whipping appts 2.1, air compressor 2.2, aeration head 2.3, settling tank 2.4, sludge reflux pump 2.5, mud valve 2.6, go out water pump 2.7, SFDANR reactor 3, intermediate water tank 3.1, recycle pump 3.2, circulation control valve 3.3, exhaust-valve 3.4, gas extractor 3.5, sealing plate 3.6, cylindrical sludge bed 3.7, water-distributing device 3.8, triphase separator 3.9, heating zone device 3.10, rising pipe 3.11, sponge filler 3.12, water distributing pore 3.13, storage basin 4, enter dredge pump 4.1.
Raw water box 1 is connected with A-O reactor 2 by former water intake pump 1.1, A-O reactor 2 is connected with settling tank 2.4 by rising pipe, be connected with the first lattice room of A-O reactor 2 by sludge reflux pump 2.5 bottom settling tank 2.4, settling tank 2.4 passes through water pump 2.7 and is connected with bottom SFDANR reactor 3, and storage basin 4 passes through to be connected into dredge pump 4.1 with bottom mud SFDANR reactor 3.
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 2.1, lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head 2.3, provide pressure by air compressor 2.2.
SFDANR reactor 3 is provided with cylindrical sludge bed 3.7, and top is provided with top sealing plate 3.6 and triphase separator 3.9, and centre is provided with temperature control heating belting 3.10, and bottom is provided with water-distributing device 3.8; Triphase separator 3.9 is connected with gas extractor 3.5 by pipeline; Cylindrical sludge bed 3.7 top is connected with bottom SFDANR reactor 3 with circulation control valve 3.2 by intermediate water tank 3.1, recycle pump 3.2; SFDANR reactor 3 water outlet is discharged by rising pipe 3.11.
Concrete test water adopts the additional bicarbonate of ammonia of Beijing University of Technology's dependents' district sanitary sewage as former water, and concrete water quality is as follows: pH is 6.8-7.3, COD concentration is 120-180mg/L, NH
4 +-N concentration is 150-220mg/L, PO
4 3-concentration is 6.2-7.8mg/L, NO
2 --N and NO
3 --N is all below detectability, and COD/N is than being 0.55-1.2.Testing mud added by every day is the fresh excess sludge (SS is 9600-12000mg/L) after certain pilot scale concentrates.A-O reactor useful volume 9L used, be divided into 9 lattice rooms, wherein first three lattice room is anaerobic zone, all the other are aerobic zone, and each lattice room is connected by water flowing duct staggered up and down on dividing plate, total hrt 7.2h, return sludge ratio 60%, the useful volume of SFDANR reactor is 5L, and hydraulic detention time is 4.8h, self-circulation reflux ratio 100%.Carrying out practically operating process is as follows:
(1) in raw water box and storage basin, high ammonia-nitrogen wastewater and fresh excess sludge is filled respectively.
(2) high ammonia-nitrogen wastewater in raw water box injects A-O reactor by former water intake pump, starts whipping appts, and regulate aerating system flow to make dissolved oxygen maintain 1.5-2.5mg/L, pH value controls to enter settling tank in the water outlet of 8.0-9.0, A-O reactor.
Before system is run continuously, first start A-O reactor, with the anaerobic-aerobic disposal mud of actual cities sewage work for inoculation mud injects A-O reactor, sludge concentration is 2000-3000mg/L; NH will be added
4hCO
3actual cities sanitary sewage pump into lattice room, A-O reactor anaerobic zone, start whipping appts subsequently, regulate aerating system flow to make dissolved oxygen maintain 1.5-2.5mg/L, control to add NH
4hCO
3concentration make influent ammonia nitrogen loading maintain 0.2-0.3kgNH
4 +-N/m
3d, pH value controls at 8.0-9.0, runs A-O reactor under these conditions, and when water outlet accumulation rate of nitrite is greater than 90% and continues maintenance 15 days, short distance nitration is achieved; Sludge retention time is made to maintain 15-20 days by controlling mud valve spoil disposal.
(3) after the mud-water separation in settling tank, supernatant liquor passes through water pump and squeezes into SFDANR reactor, and meanwhile, the fresh excess sludge in storage basin passes through to squeeze into SFDANR reactor into dredge pump, and sludge retention time maintains 15-20 days.Finally realize excess sludge and nitrification liquid ferments at SFDANR reactor, the coupling processing of denitrification and Anammox.
Before system is run continuously, first start SFDANR reactor, detailed process is: water inlet adopts NH
4 +-N:NO
2 --N is the artificial distribution of 1:1.3, initial TN concentration is 20mg/L and progressively increases nitrogen load until 200mg/L with the gradient of 20mg/L, each stage terminal be autotrophic denitrification rate more than 95% and continue maintenance more than 15 days, finally complete the Anammox acclimation to SFDANR reactor; Water inlet adopts NH
4 +-N:NO
2 --N is 1:1.3 and TN is the artificial distribution of 200mg/L, adds sodium acetate simultaneously and makes SCOD concentration be 100-150mg/L as denitrifying carbon source, when TN clearance higher than 90% and continue maintenance more than 15 days time, Anammox and denitrifying coupling successfully realize; Make SCOD concentration continue to maintain 100-150mg/L using excess sludge substituted acetic acid sodium as denitrifying carbon source, when TN clearance higher than 90% and continue maintenance more than 15 days time, reach autotrophic denitrification synchronous sludge fermentation coupling denitrification realization.
(4) after process, water outlet and mud discharge respectively by water shoot and mud valve, exhaust-valve.
Continuous print test-results shows: as SFDANR reactor sludge concentration 7000-8000mg/L, and utilize its process high ammonia-nitrogen wastewater, the pH value of final outflow water is 7.1-7.8, ammonia nitrogen concentration 1.5-6.2mg/L, total nitrogen concentration 12-25mg/L, PO
4 3-concentration is 2.3-4.2mg/L, COD value 40-60mg/L, simultaneously mud decrement about 30%.System successfully achieves synchronous sludge fermentation, sewage denitrification and autotrophic denitrification.
Claims (1)
1. a reinforcement sludge digests and the method for synchronous denitrification dephosphorizing, application is as lower device: this device comprises raw water box (1), former water intake pump (1.1), A-O reactor (2), whipping appts (2.1), air compressor (2.2), aeration head (2.3), settling tank (2.4), sludge reflux pump (2.5), mud valve (2.6), go out water pump (2.7), SFDANR reactor (3), intermediate water tank (3.1), recycle pump (3.2), circulation control valve (3.3), exhaust-valve (3.4), gas extractor (3.5), sealing plate (3.6), cylindrical sludge bed (3.7), water-distributing device (3.8), triphase separator (3.9), heating zone device (3.10), rising pipe (3.11), sponge filler (3.12), water distributing pore (3.13), storage basin (4), enter dredge pump (4.1),
Raw water box (1) is connected with A-O reactor (2) by former water intake pump (1.1), A-O reactor (2) is connected with settling tank (2.4) by rising pipe, settling tank (2.4) bottom is connected with the first lattice room of A-O reactor (2) by sludge reflux pump (2.5), settling tank (2.4) passes through water pump (2.7) and is connected with SFDANR reactor (3) bottom, and storage basin (4) passes through to be connected into dredge pump (4.1) with mud SFDANR reactor (3) bottom;
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 (2.1), lattice room, aerobic zone is divided into 4-6 lattice room, be provided with aeration head (2.3), provide pressure by air compressor (2.2);
SFDANR reactor (3) is provided with cylindrical sludge bed (3.7), top is provided with top sealing plate (3.6) and triphase separator (3.9), centre is provided with temperature control heating belting (3.10), and bottom is provided with water-distributing device (3.8); Triphase separator (3.9) is connected with gas extractor (3.5) by pipeline; Cylindrical sludge bed (3.7) top is connected with SFDANR reactor (3) bottom by intermediate water tank (3.1), recycle pump (3.2) and circulation control valve (3.2); SFDANR reactor (3) water outlet is discharged by rising pipe (3.11); It is characterized in that, comprise the following steps:
(1) A-O reactor is started: with the anaerobic-aerobic disposal mud of actual cities sewage work for inoculation mud injects A-O reactor, sludge concentration is 2000-3000mg/L, hydraulic detention time 5-8h, sludge retention time 15-25 days; NH will be added
4hCO
3actual cities sanitary sewage pump into lattice room, A-O reactor anaerobic zone, start whipping appts subsequently, regulate aerating system flow to make dissolved oxygen maintain 1.5-2.5mg/L, control to add NH
4hCO
3concentration make influent ammonia nitrogen loading maintain 0.2-0.3kgNH
4 +-N/m
3d, pH value controls at 8.0-9.0, and water outlet enters settling tank, and precipitating sludge is back to the first lattice room of A-O reactor, and control of reflux ratio is at 50%-100%; Run A-O reactor under these conditions, when water outlet phosphate concn lower than 0.5mg/L and accumulation rate of nitrite be greater than 90% continue maintenance 15 days time, dephosphorization process and short distance nitration are achieved;
(2) start SFDANR reactor: sludge concentration 7000-8000mg/L in control SFDANR reactor, hydraulic detention time 3-5h, sludge retention time 10-20 days, water inlet adopts NH
4 +-N and NO
2 --N mass ratio is the artificial distribution of 1:1.3, initial TN concentration is 20mg/L and progressively increases nitrogen load until 200mg/L with the gradient of 20mg/L, the time point of each increase nitrogen load is that autotrophic denitrification rate continues maintenance more than 15 days more than 95%, finally completes the Anammox acclimation to SFDANR reactor; Water inlet adopts NH
4 +-N and NO
2 --N mass ratio is 1:1.3 and TN is the artificial distribution of 200mg/L, add sodium acetate makes SCOD concentration be 100-150mg/L as denitrifying carbon source simultaneously, when TN clearance higher than 90% and continue maintenance more than 15 days time, Anammox and denitrifying coupling successfully realize; Make SCOD concentration continue to maintain 100-150mg/L using excess sludge substituted acetic acid sodium as denitrifying carbon source, when TN clearance higher than 90% and continue maintenance more than 15 days time, reach autotrophic denitrification synchronous sludge fermentation coupling denitrification realization;
A ?after O reactor and SFDANR reactor complete startup respectively, by whole device series operation: the high ammonia-nitrogen wastewater in raw water box by former water intake pump squeeze into A ?O reactor, sludge concentration be 2000 ?3000mg/L, hydraulic detention time 5 ?8h, sludge retention time 15 ?25 days, start whipping appts subsequently, regulate aerating system flow make dissolved oxygen maintain 1.5 ?2.5mg/L, pH value control 8.0 ?9.0, A ?the water outlet of O reactor enter settling tank, after mud-water separation, precipitating sludge be back to A ?the first lattice room of O reactor, control of reflux ratio 50% ?100%, supernatant liquor enters SFDANR reactor by water outlet infusion, simultaneously, fresh excess sludge in storage basin passes through to inject SFDANR reactor into dredge pump, in control SFDANR reactor sludge concentration 7000 ?8000mg/L, hydraulic detention time 3 ?5h, sludge retention time 10 ?20 days, self-circulation reflux ratio 80% ?150%, finally realize excess sludge and nitrification liquid ferments at SFDANR reactor, the coupling processing of denitrification and Anammox, water outlet after process and mud are respectively by water shoot and mud valve, exhaust-valve discharges.
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| CN104230105B (en) * | 2014-09-12 | 2016-04-27 | 河南师范大学 | A kind of municipal domestic sewage treatment device and operation method thereof |
| CN105254134B (en) * | 2015-11-16 | 2017-07-28 | 天津城建大学 | Biological denitrificaion is combined the unit |
| CN108483807B (en) * | 2018-04-12 | 2024-02-09 | 广西玉林市大智环保工程有限公司 | Device and method for municipal sewage denitrification and dephosphorization coupled sludge reduction |
| CN108675450B (en) * | 2018-05-07 | 2021-01-05 | 北京工业大学 | Device and method for realizing efficient and low-consumption nitrogen and phosphorus removal of municipal sewage |
| CN109387390B (en) * | 2018-11-23 | 2022-04-15 | 江苏大学 | Sediment anaerobic incubator |
| CN112408601B (en) * | 2020-11-13 | 2022-08-19 | 北京工业大学 | Two-stage self-circulation separate aeration combined tower for treating nitrogen-containing wastewater containing organic matters |
| CN113933372B (en) * | 2021-11-11 | 2023-11-03 | 广西大学 | Quantitative identification method for river basin nitrate nitrogen source river entering load and river entering coefficient |
| CN114772887B (en) * | 2022-04-11 | 2023-07-21 | 同济大学 | Method for improving methane yield of anaerobic sludge digestion by using ammonium bicarbonate |
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| CN101880115B (en) * | 2010-02-03 | 2012-12-26 | 王鹤立 | Method for supplementing denitrifying carbon source by utilizing excess sludge ethanol-type fermentation |
| CN102531174B (en) * | 2012-03-02 | 2014-02-19 | 北京工业大学 | Method for reducing amount of sludge of improved sewage factory and performing low-carbon-consumption denitrification |
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