CN102583900A - Method for removing nitrogen and phosphorus by MBBRs (Moving Bed Biofilm Reactors) with sectionalized water inflow - Google Patents
Method for removing nitrogen and phosphorus by MBBRs (Moving Bed Biofilm Reactors) with sectionalized water inflow Download PDFInfo
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Abstract
A method for removing nitrogen and phosphorus by MBBRs (Moving Bed Biofilm Reactors) with sectionalized water inflow belongs to the field of sewage treatment. The MBBRs at first, second and third sections are divided into three sections, a sand disc aerator is arranged at the bottom of each MBBR, a bearing layer is arranged above each sand disc aerator, and a filling area is arranged above each bearing layer; hollow spheres are adopted as fillers, and the specification specific surface area of the hollow sphere ranges from 400m<2>/m<3> to 500m<2>/m<3>; and the filling volume of the fillers ranges from 15% to 45%. According to the method, the improved sectionalized water inflow technology is combined with fluidized bed biofilms, and the technology has the advantages of resisting shock load, strengthening SND (Shortcut Nitrification and Denitrification) denitrification, saving energy and reducing consumption by combination of activated sludge and the fluidized bed biofilms. Therefore, the method is applicable to the field of deep nitrogen and phosphorus removing on domestic sewage and industrial sewage in large, middle and small cities and towns.
Description
Technical field
The present invention relates to a kind of improvement segmental influent and biological denitrification dephosphorization process; Belong to technical field of biological sewage treatment by using; It will be improved segmental influent technology and combine with MBBR; The coupling of active sludge and fluidized bed bio film makes this technology have anti-shock loading simultaneously, strengthens the SND denitrogenation, energy-saving and cost-reducing advantage, is applicable to large, medium and small type town domestic sewage and trade effluent advanced nitrogen dephosphorization field.
Background technology
Even flow segmental influent technology is a kind of technology of bio-denitrifying sewage efficiently; It is domestic and international in recent years biological denitrification process newly developed; It is coupled traditional AO technology, UCT technology; The mode that adopts multipoint water feeding is the biological treatment that adopts activated sludge process in each section anaerobic zone, oxygen-starved area water inlet.
Along with the increasingly stringent of emission standard, single technology can not satisfy Times'Demand far away, the series connection of coupling technique, collaborative becomes more and more important.The present invention relates to the combined action of activated sludge process and fluidized bed bio embrane method, the advantage exploitation is a kind of to the low C/N sewage treatment process more favourable than municipal effluent separately in conjunction with both.
Biomembrance process---biological contact oxidation reactor, the filler outside surface directly contacts with gas, liquid and dissolved oxygen is higher, and microbial population is main with aerobic bacteria, nitrifier; The filler internal layer is because the oxygen transmission is obstructed and external oxygen has been formed the anoxic microenvironment by mass consumption; Denitrifying bacteria is preponderated; Each carrier all is a microreactor like this, and nitration reaction and anti-nitration reaction are existed simultaneously, therefore through the inner dissolved oxygen environment of control mud decrement device; Make synchronous nitration denitrification denitrogenation act in the contact oxidation reactor and strengthened, thereby improved treatment effect.This technology has processing power efficiently, and the characteristic principle analysis is following: 1. mass transfer condition is good, in contact oxidation method because the stirring of air; The sewage of whole oxidation pond flows between filler; Make the bigger speed of relative movement of generation between microbial film and the current, the medium of having accelerated bacterium surface upgrades, and has strengthened mass transfer effect; Accelerate biological metabolism speed, shortened the treatment time.2. oxygen-transfer efficiency is high, the corresponding raising of organic oxidation rate.The filler of contact oxidation method has the effect of promoting oxidation effect, and dynamicefficiency is at 3kgO
2/ kw improves 30% than packless aeration.3. higher biological concentration is arranged.The sludge concentration of general activated sludge process is 2～3g/L, and contact oxidation method can reach 10～20g/L.Because microorganism concn is high, so improved BOD greatly
5Volumetric loading and processing efficiency.Biological contact oxidation process has many advantages; Be a kind of structures of biochemical treatment efficiently, but also exist some shortcomings: biomembranous thickness increases and increases with load, and the too high then microbial film of loading is blocked up; Cause that filler stops up, and need have anticlogging flushing measure.Filler and support etc. often cause construction cost to increase.
Activated sludge process---active sludge all is the cotton-shaped microorganisms symbiosis body of baroque macroscopic suede that is made up of various mikrobes, organism and mineral colloid, suspended substance.Such symbiote has very strong adsorptive power and degradation capability, and a lot of pollutent that can adsorb and degrade can reach the purpose of handling and purifying waste water, and is modal sewage treatment.Activated sludge process is simple to operate flexibly, plurality of advantages such as wide adaptability, but the discharging excess sludge production big, be subject to problems such as external environment influence, processing efficiency be not high and impel that investigators constantly explore, the exploitation novel process.
MBBR---improves living weight and biological species in the reactor drum through in reactor drum, adding the suspending carrier of some amount, thereby improves the processing efficiency of reactor drum.Because packing density approaches water, so in aeration, be complete admixture with water, the environment of microorganism growth is the gas, liquid, solid three-phase.Collision and the shearing action of carrier in water makes air bubble more tiny, increased the utilization ratio of oxygen.MBBR technology has the advantage of traditional fluidized-bed and biological contact oxidation process concurrently; Be a kind of new and effective sewage water treatment method, the aeration in the dependence aeration tank and the castering action of current make carrier be in fluidized state, and then form the active sludge of suspension growth and the microbial film of apposition growth; This just makes moving-bed biofilm use the whole reactor space; Give full play to and adhere to mutually and both meliority of suspending phase biology, make it to maximize favourable factors and minimize unfavourable ones, replenish each other.
The synchronous nitration and denitrification phenomenon can be explained from microenvironment theory and biology two aspects.The microenvironment theory is thought: because there is multiple microenvironment type in the ununiformity of microbial species group structure, species distribution and biochemical reaction in active sludge zoogloea inside and microbial film inside.Because the restriction of oxygen diffusion produces the dissolved oxygen gradient in mikrobe flco or microbial film, its outside surface dissolved oxygen is higher, is main with aerobic bacteria, nitrifier; Dark people's flco or microbial film are inner, and the oxygen transmission is obstructed and the mass consumption of external oxygen, produces the oxygen-starved area, even anaerobic zone, and denitrifying bacteria is preponderated.The level of dissolved oxygen in the controlling reactor, adjustment anoxic anaerobism microenvironment and the shared ratio of aerobic environment, thus promote denitrification, reach the purpose of denitrogenation.It is theoretical that biological explanation is different from traditional denitrogenation, and existing report has found that many heterotrophic microorganisms can carry out nitrification to organic and inorganic nitrogen-containing compound.Compare with the autotrophy nitrifier, the heterotrophic nitrification bacteria growing is fast, and output is high, can stand lower dissolved oxygen concentration and sourer environment.Other there are some researches show that most of nitrification bacterias also are aerobic denitrifying bacterias simultaneously, and notions such as aerobic denitrification and autotrophic denitrification are proposed in succession, has established the theoretical basis of synchronous nitration and denitrification reaction biological denitrificaion new technology.
Summary of the invention
Even flow segmental influent denitrification dephosphorization technique has denitrification dephosphorization performance and efficient denitrification preferably, for the sewage than low ratio of carbon to ammonium certain processing advantage is arranged.The present invention combines even flow segmental influent technology and MBBR technology, utilizes and strengthens the coupling technique that synchronous nitration denitrification denitrogenation is used for seeking low ratio of carbon to ammonium sewage realization optimal treatment effect.
A kind of device of segmental influent MBBR denitrogenation dephosphorizing, it is formed as follows:
Connect raw water box, intake pump and main body bio-reactor by water inlet pipe, the main body bio-reactor is connected with settling tank, and settling tank is connected with first section anoxic reacter through reflux pump, vacuum breaker, and supernatant is discharged from water outlet; The perforate dividing plate is divided into 7 zones with the main body bio-reactor, and dividing plate is provided with pipe; Be respectively anaerobic reactor, first section anoxic reacter, first section fluidized bed bio membrane reactor, second section anoxic reacter, second section fluidized bed bio membrane reactor, the 3rd section anoxic reacter, stage fluidized bed biofilm reactor along the water inlet direction.Control the segmental influent pump with three sections entering systems of former moisture through system, respectively anaerobic reactor, second section anoxic reacter, the 3rd section anoxic reacter; Be provided with whisking appliance in anaerobic reactor, first section anoxic reacter, second section anoxic reacter, the 3rd section anoxic reacter; First section anoxic reacter is communicated with anaerobic reactor through reflux pump; Said first section fluidized bed bio membrane reactor, second section fluidized bed bio membrane reactor, each bottom, lattice chamber of stage fluidized bed biofilm reactor are equipped with aerator; Aerator is connected with intake valve, spinner-type flowmeter, air, constitutes aerating system; Place the DO transmitter in first, second and third section fluidized bed bio membrane reactor, by the control of DO on-Line Monitor Device, segmentation section intake pump is controlled by the PID unit.
It is characterized in that: divide 3 parts in the fluidized bed bio membrane reactor, the bottom is the emery disc aerator, and there is supporting layer the aerator top, is the packing area on the supporting layer; The used material of filler is a hollow ball, specification
Specific surface area 400-500m
2/ m
3The filler packing volume is than being 15-45%;
A kind of method of segmental influent MBBR denitrogenation dephosphorizing is characterised in that:
(1) unit comes the regulating flow distribution system; Unstable state through water inlet phase angle variations, cycle change, sinusoidal Wave crest and wave trough changes three sections intake pump flows of control changes; Under the water yield is impacted; Realize that sludge loss minimizes and biological treatment stable through allotment, realize that the adjustment operating parameter is energy-conservation in real time three sections water inlet different flows.
(2) sewage of raw water box gets into anaerobic reactor, second section anoxic reacter and the 3rd section anoxic reacter through intake pump, segmental influent pump for three sections following minute of the regulation and control of system successively.PolyP bacteria is released phosphorus in the anaerobic reactor; Contain a large amount of phosphatic water outlets and get into first section anoxic reacter; First section anoxic reacter water outlet gets into first section fluidized bed bio membrane reactor; The pressurized air that is provided by air gets into aerator through spinner-type flowmeter, is this regional oxygen supply, through DO transmitter and the monitoring of DO on-Line Monitor Device; First section fluidized bed bio membrane reactor water outlet gets into second section anoxic reacter, and the water outlet of second section fluidized bed bio membrane reactor gets in the 3rd section anoxic reacter, under the effect of whisking appliance and former water thorough mixing; Second section anoxic reacter water outlet gets into second section fluidized bed bio membrane reactor, and the 3rd section anoxic reacter water outlet gets into stage fluidized bed biofilm reactor, utilizes the microbial film " microenvironment " on the filler to make synchronous nitration denitrification denitrogenation be achieved; Stage fluidized bed biofilm reactor water outlet gets into settling tank, and a part is discharged from water outlet, and a part is back to first section anoxic reacter through reflux pump; First section anoxic reacter mud gets into anaerobic reactor through reflux pump, and there is extremely superior condition of compatibility in this system to the sewage of C/N.
(3) through the denitrifying bacteria effect, reacted water outlet gets into the fluidized bed bio membrane reactor to former water labile organic compound in anoxic reacter.Fluidized bed bio membrane reactor inner control DO is 0.5-1.0mg/L; The water inlet fluidised form that goes out on advancing down makes sewage under the stirring of air, fully contact with filler; Activated sludge process and biomembrance process combine and make a large amount of enrichments of autotrophy nitrifier, and the nitrated performance of technology is strengthened.Sludge age is 12-20 days, and hydraulic detention time is 8-10 hour, and return sludge ratio is 70%-100%, and internal reflux ratio is 75%-100%, and no nitrification liquid refluxes.Reactor bottom is provided with the emery disc aerator, even gas distribution water distribution, and flooding velocity 7-9L/h, 20-24 ℃ of temperature control, system is moving under continuously normal water inlet condition, promptly accomplishes the extension membrane process after 4-6 days.
A kind of apparatus and method of segmental influent MBBR denitrogenation dephosphorizing compared with prior art have following effect:
(1) the MBBR oxygen-transfer efficiency is high, and collision and the shearing action of carrier in water makes air bubble more tiny, increased the utilization ratio of oxygen, and dynamicefficiency improves 30% than packless aeration, and does not need nitrification liquid to reflux, and practices thrift the power consumption of aeration and pump.
(2) rationally control the dissolved oxygen concentration of contact-oxidation pool; Utilize biological film formed " microenvironment " of adhering on the hollow ball to realize synchronous nitration denitrification denitrogenation; In conjunction with segmental influent technology and denitrification dephosphorization, further enlarged segmental influent MBBR coupling technique on the former water carbon source basis to the range of application of low C/N making full use of than sewage.
(3) multipoint water feeding makes system to the demand of dissolved oxygen balance more, and effectively avoids or mud is washed away when reducing peak discharge danger, and stronger anti-shock loading performance is arranged.
Description of drawings
Fig. 1 is a device synoptic diagram of the present invention
Among the figure, the 1-raw water box; The 2-intake pump; 3-segmental influent pump; The 4-anaerobic reactor; First section anoxic reacter of 5-; First section contact oxidation reactor of 6-; Second section anoxic reacter of 7-; Second section contact oxidation reactor of 8-; The 3rd section sampling of 9-reactor drum; The 3rd section contact oxidation reactor of 10-; The 11-unit; The 12-whisking appliance; The 13-DO on line control system; The 14-air; The 15-air control valve; 16-mixed-liquor return pump; 17-emery disc aerator; The 18-spinner-type flowmeter; The 19-sludge reflux pump; The 20-variable valve; The 21-second pond; The 22-water outlet; The 23-DO transmitter.
Embodiment
The present invention connects raw water box, intake pump and main body bio-reactor by water inlet pipe, and the main body bio-reactor is connected with settling tank, and settling tank is connected with first section anoxic reacter through reflux pump, vacuum breaker, and supernatant is discharged from water outlet; The perforate dividing plate is divided into 7 zones with the main body bio-reactor, and dividing plate is provided with pipe; Be respectively anaerobic reactor, first section anoxic reacter, first section fluidized bed bio membrane reactor, second section anoxic reacter, second section fluidized bed bio membrane reactor, the 3rd section anoxic reacter, stage fluidized bed biofilm reactor along the water inlet direction.Control the segmental influent pump with three sections entering systems of former moisture through system, respectively anaerobic reactor, second section anoxic reacter, the 3rd section anoxic reacter; Be provided with whisking appliance in anaerobic reactor, first section anoxic reacter, second section anoxic reacter, the 3rd section anoxic reacter; First section anoxic reacter is communicated with anaerobic reactor through reflux pump; Said first section fluidized bed bio membrane reactor, second section fluidized bed bio membrane reactor, each bottom, lattice chamber of stage fluidized bed biofilm reactor are equipped with aerator; Aerator is connected with intake valve, spinner-type flowmeter, air, constitutes aerating system; Place the DO transmitter in first, second and third section fluidized bed bio membrane reactor, by the control of DO on-Line Monitor Device, segmentation section intake pump is controlled by the PID unit.
The present invention provides a kind of method that improves segmental influent bio-contact oxidation denitrogenation dephosphorizing, is characterised in that:
(1) unit comes the regulating flow distribution system; Unstable state through water inlet phase angle variations, cycle change, sinusoidal Wave crest and wave trough changes three sections intake pump flows of control changes; Under the water yield is impacted; Realize that sludge loss minimizes and biological treatment stable through allotment, realize that the adjustment operating parameter is energy-conservation in real time three sections water inlet different flows.
(2) sewage of raw water box gets into anaerobic reactor, second section anoxic reacter and the 3rd section anoxic reacter through intake pump, segmental influent pump for three sections following minute of the regulation and control of system successively.PolyP bacteria is released phosphorus in the anaerobic reactor; Contain a large amount of phosphatic water outlets and get into first section anoxic reacter; First section anoxic reacter water outlet gets into first section fluidized bed bio membrane reactor; The pressurized air that is provided by air gets into aerator through spinner-type flowmeter, is this regional oxygen supply, through DO transmitter and the monitoring of DO on-Line Monitor Device; First section fluidized bed bio membrane reactor water outlet gets into second section anoxic reacter, and the water outlet of second section fluidized bed bio membrane reactor gets in the 3rd section anoxic reacter, under the effect of whisking appliance and former water thorough mixing; Second section anoxic reacter water outlet gets into second section fluidized bed bio membrane reactor, and the 3rd section anoxic reacter water outlet gets into stage fluidized bed biofilm reactor, utilizes the microbial film " microenvironment " on the filler to make synchronous nitration denitrification denitrogenation be achieved; Stage fluidized bed biofilm reactor water outlet gets into settling tank, and a part is discharged from water outlet, and a part is back to first section anoxic reacter through reflux pump; First section anoxic reacter mud gets into anaerobic reactor through reflux pump, and there is extremely superior condition of compatibility in this system to the sewage of C/N.
(3) through the denitrifying bacteria effect, reacted water outlet gets into the fluidized bed bio membrane reactor to former water labile organic compound in anoxic reacter.Fluidized bed bio membrane reactor inner control DO is 0.5-1.0mg/L; The water inlet fluidised form that goes out on advancing down makes sewage under the stirring of air, fully contact with filler; Activated sludge process and biomembrance process combine and make a large amount of enrichments of autotrophy nitrifier, and the nitrated performance of technology is strengthened.Sludge age is 12-20 days, and hydraulic detention time is 8-10 hour, and return sludge ratio is 70%-100%, and internal reflux ratio is 75%-100%, and no nitrification liquid refluxes.Reactor bottom is provided with the emery disc aerator, even gas distribution water distribution, and flooding velocity 7-9L/h, 20-24 ℃ of temperature control, system is moving under continuously normal water inlet condition, promptly accomplishes the extension membrane process after 4-6 days.
With dependents' district, Beijing real life sewage is process object, COD=180-245mg/L, TN=27-77mg/L; TP=4.01-5.32mg/L; C/N=1.63-6.23, hydraulic detention time 8h, sludge age 13-20d; Hang the film success through 6 days fluidized bed bio membrane reactors, the 15d system is stable.Average sludge concentration 3100 ± 150mg/L, DO is controlled at 0.5-1.0mg/L, return sludge ratio 100%, internal reflux ratio 75%, temperature are controlled at about 22 ℃.Start stable back and move 3 months continuously, test-results shows, water outlet COD=27-43mg/L, TN=9.07-14.1mg/L, TP=0.29-0.48mg/L, NH
4 +-N is less than 1mg/L.System is stable to TN, TP removal effect, and test-results reaches town sewage one-level A emission standard.
Case 2
With the preliminary sedimentation tank water outlet of Beijing sewage work is process object, COD=180-453mg/L, TN=33-71mg/L; TP=1.01-7.32mg/L, C/N=2.01-7.20, hydraulic detention time 9h; Sludge age 13-20d, average sludge concentration 4500 ± 150mg/L, DO is controlled at 0.5-1.0mg/L; Return sludge ratio 100%, internal reflux ratio 75%, temperature are controlled at about 20 ℃.Start stable back and move 3 months continuously, test-results shows, water outlet COD=22-48mg/L, TN=6.3-13.9mg/L, TP=0.14-0.38mg/L, NH
4 +-N is less than 1mg/L.System is stable to TN, TP removal effect, and test-results reaches town sewage one-level A emission standard.
Claims (1)
1. the method for a segmental influent MBBR denitrogenation dephosphorizing; Use like lower device: connect raw water box (1), intake pump (2) and main body bio-reactor by water inlet pipe; The main body bio-reactor is connected with settling tank (21); Settling tank (21) is connected with first section anoxic reacter (12) through reflux pump (19), vacuum breaker (20), and supernatant is discharged from water outlet (22); The perforate dividing plate is divided into 7 zones with the main body bio-reactor, and dividing plate is provided with pipe; Be respectively anaerobic reactor (4), first section anoxic reacter (5), first section fluidized bed bio membrane reactor (6), second section anoxic reacter (7), second section fluidized bed bio membrane reactor (8), the 3rd section anoxic reacter (9), stage fluidized bed biofilm reactor (10) along the water inlet direction; Control segmental influent pump (3) with three sections entering systems of former moisture through system (11), respectively anaerobic reactor, second section anoxic reacter, the 3rd section anoxic reacter; Be provided with whisking appliance (12) in anaerobic reactor (4), first section anoxic reacter (5), second section anoxic reacter (7), the 3rd section anoxic reacter (9); First section anoxic reacter (5) is communicated with anaerobic reactor (4) through reflux pump (16); Said first section fluidized bed bio membrane reactor (6), second section fluidized bed bio membrane reactor (8), each bottom, lattice chamber of stage fluidized bed biofilm reactor (10) are equipped with aerator (17); Aerator (17) is connected with intake valve (15), spinner-type flowmeter (18), air (14), constitutes aerating system; Place DO transmitter (23) in first, second and third section fluidized bed bio membrane reactor, by DO on-Line Monitor Device (13) control, segmentation section intake pump (3) is controlled by the PID unit;
It is characterized in that:
First, second and third section fluidized bed bio membrane reactor divides 3 parts, and the bottom is the emery disc aerator, and there is supporting layer the aerator top, is the packing area on the supporting layer; The used material of filler is a hollow ball, specification
Specific surface area 400-500m
2/ m
3The filler packing volume is than being 15-45%;
The sewage of raw water box (1) gets into anaerobic reactor (4), second section anoxic reacter (7) and the 3rd section anoxic reacter (9) through intake pump (2), segmental influent pump (3) for three sections following minute of the regulation and control of system (11) successively; The interior polyP bacteria of anaerobic reactor (4) is released phosphorus; Contain a large amount of phosphatic water outlets and get into first section anoxic reacter (5); First section anoxic reacter (5) water outlet gets into first section fluidized bed bio membrane reactor (6); The pressurized air that is provided by air (14) gets into aerator (17) through spinner-type flowmeter (18), is this regional oxygen supply, through DO transmitter (23) and DO on-Line Monitor Device (13) monitoring; First section fluidized bed bio membrane reactor (6) water outlet gets into second section anoxic reacter (7), and second section fluidized bed bio membrane reactor (8) water outlet gets in the 3rd section anoxic reacter (9), under the effect of whisking appliance (12) and former water thorough mixing; Second section anoxic reacter (7) water outlet gets into second section fluidized bed bio membrane reactor (8); The 3rd section anoxic reacter (9) water outlet gets into stage fluidized bed biofilm reactor (10), utilizes the microbial film " microenvironment " on the filler to make synchronous nitration denitrification denitrogenation be achieved; Stage fluidized bed biofilm reactor (10) water outlet gets into settling tank (21), and a part is discharged from water outlet (22), and a part is back to first section anoxic reacter (5) through reflux pump (19); First section anoxic reacter (5) mud gets into anaerobic reactor (4) through reflux pump (16);
Fluidized bed bio membrane reactor inner control DO is 0.5-1.0mg/L, and sludge age is 12-20 days, and hydraulic detention time is 8-10 hour, and return sludge ratio is 70%-100%, and internal reflux ratio is 75-100%, flooding velocity 7-9L/h, 20-24 ℃ of temperature control.
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| CN102826715A (en) * | 2012-09-12 | 2012-12-19 | 同济大学 | Sewage treatment method for nitrogen and phosphorus removal through combination of biofilm process and multilevel activated sludge process |
| CN102964035A (en) * | 2012-12-06 | 2013-03-13 | 北京城市排水集团有限责任公司 | Device for autotrophic nitrogen removal of composite biological membrane and operation method |
| CN103755095A (en) * | 2014-01-14 | 2014-04-30 | 江苏裕隆环保有限公司 | Nitrogen and phosphorus removal method coupling A/O step-feed MBBR (moving bed biofilm reactor) process with cloth filter |
| CN104071897A (en) * | 2014-07-21 | 2014-10-01 | 太原理工大学 | Coking wastewater treatment process by step water inlet multistage anoxic/aerobic biofilm process |
| CN105084534A (en) * | 2015-09-09 | 2015-11-25 | 青岛思普润水处理股份有限公司 | Post-denitrification operation method based on moving bed biofilm reactors (MBBRs) |
| CN107915312A (en) * | 2017-11-21 | 2018-04-17 | 中国市政工程中南设计研究总院有限公司 | A kind of continuous stream intermittent aerating biomembrane denitrogenation dephosphorization apparatus and method |
| CN108383330A (en) * | 2018-03-29 | 2018-08-10 | 陕西朗正环保科技有限公司 | A kind of decentralized type sewage processing unit |
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| 葛士建等: ""分段进水脱氮除磷工艺中反硝化除磷的实现与维持"", 《化工学报》, vol. 62, no. 9, 30 September 2011 (2011-09-30) * |
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