CN110304791A - Sewage imitates self-purification system and method - Google Patents
Sewage imitates self-purification system and method Download PDFInfo
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- 239000010802 sludge Substances 0.000 claims abstract description 56
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- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 42
- 239000011574 phosphorus Substances 0.000 claims abstract description 42
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The present invention relates to advanced nitrogen dephosphorization under a kind of town sewage advanced purification system and method more particularly to C/N ratio or cryogenic conditions.By extending biochemical section HRT to 23h-34h, the preposition compound pre-acidified area of filler increases small molecule volatile acid, anoxic, aerobic strengthened denitrification are set after being aerated section, reduces settling zone surface loading and the optimization on pool structure is provided to measures such as 0.3-0.8m/h for advanced nitrogen dephosphorization.In the method for operation, control aerobic zone dissolved oxygen keeps biochemistry pool water outlet ammonia nitrogen 2-4mg/L to control aeration quantity, promotes Nitrogen/Phosphorus Removal in 0.1-0.5mg/L, ORP current potential -10-20mV.By improving sludge concentration to 6-15g/L, 7-9m is arrived deeply to reduce land occupation in effective pond.Technology and method of the present invention, it can be in influent COD/TN in 3.0-4.0, at 5-12 DEG C of temperature, cooperation is filtered without medicament coagulating sedimentation, and guarantee TN, TP, COD removal rate keeps aeration energy consumption lower than 0.09kW/t respectively 90%, 99.5%, 93% or more, it is excellent with effluent quality, operating cost is low, the advantages such as convenient for management, and application prospect is extensive.
Description
Technical field
The invention belongs to sewage treatment fields more particularly to a kind of sewage to imitate self-purification system and method.
Background technique
Studying from nature, domestic sewage processing system are construed as a kind of removed with organic matter and specific nutrition element and are
The microbial ecosystem of purpose artificial-strengthening.Sanitary sewage enters in natural ecosystems (by taking river as an example), Natural Circulation
The self-purification function of system does not distinguish low ratio of carbon to ammonium, high-carbon nitrogen ratio sewage, and under cryogenic conditions, self-cleaning can be achieved under hot conditions
(the predominantly removal of organic matter and nitrogen phosphorus), during supply of the river water to underground water, during this also not necessarily
The removal of SS (suspended matter) phosphorus need can be realized by adding for chemical agent.This rethinks sewage treatment for us
The design of factory has good reference.From this angle, in reactor design, more consideration is given to Microbial ecosystems
The moving law and operational process of system are expected to reduction chemical agent and add, strengthen to low temperature, low carbon-nitrogen ratio sewage water quality is answered
It is right, operation energy consumption is reduced, realizes more excellent treatment efficiency.
The amount that the contaminated reason in river is construed as being discharged into the pollutant in river has been more than river ecosystem
Self-purification capacity, the biochemical reaction in sewage disposal system are understood to first order kinetics process mostly, and existing sewage treatment system
In system design, in order to reduce land occupation, cost of investment is reduced, often uses higher load, from the angle of kinetics,
As soon as the selection of this parameter can be such that reaction process maintains compared on high reaction rate, but higher reaction rate is also meaned
Reaction it is incomplete, to bring COD (COD) removal, denitrogenation or phosphor-removing effect it is incomplete.
Different from industrial wastewater, the overwhelming majority of sanitary sewage is defined as the ingredient of organic contamination or inorganic pollution
(except humic acid, outside the ingredients such as humus) can be removed away from water body by the good utilization of microorganism or conversion.From this
A angle is set out the metabolic process of during sanitary sewage disposal enhancement microbiological, and microbial ecosystem is given full play to out
Efficiency realizes that deep purification of waste water is feasible, also will be economical in operating cost.
Currently, with the development of China's economic society, the amount of the pollutant of anthropogenic discharge increases sharply, simultaneously because to life
State water, wetland, a large amount of utilizations in soil etc. cause the decline of natural ecosystems self-purification capacity, objectively in order to maintain
The ecosystem relatively suitable human living level, country put into effect the effluent-disposal standard being increasingly stringenter.However, existing
Pursuit high efficiency, Low investment cost sewage-treating reactor tend not to reach these discharge marks in actual moving process
Standard, this to have in existing sewage disposal process to add the further denitrogenation of the forms such as carbon source using denitrification filter pool；It adopts
With further dephosphorization of processes such as coagulating sedimentation filterings；Using coagulating sedimentation, the technologies such as film filtering further remove COD.These are arranged
The effect that can play advanced treating is applied, but also brings the problems such as medicament is costly, and carbon emission amount is high in treatment process, from whole
For the protection of a ecosystem, the cost (resource consumption, chemicals production carbon emission) and benefit of these materializing strategy measures
Whether (purification of water quality, reducing influences natural ecosystems) is positive to need further deeply to calculate and evaluate.
In terms of the developing history of sewage disposal system, whether activated sludge process or SBR (sequencing batch active sludge)
Equal sewage treatment process are COD at the beginning of initiative, are not denitrogenation based on ammonia nitrogen, based on dephosphorization, subsequent anoxic zone or
The addition of anoxia stirring and anaerobic zone makes it have the function of denitrogenation dephosphorizing, but there is no the demands from advanced nitrogen dephosphorization
It sets out, reactor design, to guarantee efficient Nitrogen/Phosphorus Removal.
Due to the setting of septic tank, China's sanitary sewage is in the state of low ratio of carbon to ammonium mostly, and low-carbon is considered than situation
An important factor for being limitation sewage water denitrification effect.From this premise, the setting of denitrification filter pool, which also just becomes, necessarily to be selected
It selects.But from the point of view of the relevant microbial metabolism of denitrogenation, nitration denitrification, short-cut nitrification and denitrification, short-cut denitrification coupling
Anammox, the processes such as Anammox are generally existing in natural ecosystems, and in the circulation of natural nitrogen
It play an important role.Wherein, from above-mentioned nitration denitrification, short-cut nitrification and denitrification to Anammox, microbial metabolism
Needed for the amount of organic matter also successively reduce from high to low, theoretically, anaerobic ammonium oxidation process does not need carbon source.Have benefited from
Natural ecosystems couple Anammox to short distance nitration short-cut denitrification, short-cut denitrification, the processes such as Anammox
It utilizes, in the self purification process of natural ecosystems and the problem of there is no low-carbons than influencing denitrification process.From microbial metabolism
Angle set out, in nitration denitrification, short-cut nitrification and denitrification, short-cut denitrification couples Anammox, Anammox
During carbon source is successively decreased, the rate efficiency of microorganism is also further decreased.In existing sewage disposal system, anti-nitre is nitrified
The process of change is generally existing, and is widely used, but short distance nitration short-cut denitrification, anaerobic ammonium oxidation process are removed in sewage water denitrification
It is not played an important role but in phosphorus system.To find out its cause, the unpromising short distance of the setting of existing sewage-treating reactor
Short-cut denitrification is nitrified, anaerobic ammonium oxidation process provides condition advantageous enough, can not be enriched with out enough short distance nitration bacterium, and
Anaerobic ammonia oxidizing bacteria generates enough nitrite.In terms of the metabolic demand of Anammox and ecological niche, relative to denitrification
Bacterium, advantageous growth conditions (ecological niche) is low ratio of carbon to ammonium, low dissolved oxygen, long sludge age, long hydraulic detention time, low negative
The conditions such as lotus or high ammonia nitrogen, and existing sewage disposal system is not with these conditions.
From the reply angle of low temperature, low temperature can not kill microorganism, only produce to its enzyme activity and metabolic process
It is raw to influence, its metabolic capability is reduced, in this case, extends the residence time, the reply to hypothermic phase can be realized.
Even if should be ensured that carbon sources more as far as possible by denitrification in biochemical reaction process from the angle of nitration denitrification
Process utilizes, and reduces its utilization by Aerobic, however in existing treatment process, although denitrification zone absorbs
Most of carbon source, but due to the high-solubility oxygen of aerobic zone and the dissolved oxygen brought by nitrification liquid reflux, make one into water
Point carbon source is converted into CO by aeration process2It is consumed with water, there is no being utilized as denitrifying carbon source, this exacerbates carbon
Nitrogen ratio it is unbalance, and solve the problems, such as this approach be reduce dissolved oxygen concentration, make nitration denitrification process same
It is synchronous as far as possible in reactor to occur, reduce direct oxidation process of the organic matter using oxygen as electron acceptor.
Summary of the invention
In view of this, one of main object of the present invention is to propose that a kind of sewage imitates self-purification system and method, with
Phase at least is partially solved at least one of above-mentioned technical problem.
To achieve the goals above, as one aspect of the present invention, a kind of imitative self-purification system of sewage, packet are provided
It includes:
Level-one anaerobic zone which is provided with level-one anaerobic zone water inlet and level-one anaerobic zone water outlet；
Anoxic zone, which is provided with anoxic zone water inlet and anoxic zone water outlet and anoxic zone water inlet goes out with level-one anaerobic zone
Mouth of a river connection；
Main reaction region which is provided with main reaction region water inlet and main reaction region water outlet and main reaction region water inlet and anoxic
The connection of area's water outlet；And
Settling zone joins with settling zone water inlet and bio-chemical effluent mouth, settling zone water inlet and main reaction region water outlet thereon
It is logical.
As another aspect of the present invention, provide a kind of using the net of purification system as described above progress sewage treatment
Change method, includes the following steps:
(1) water quality to be processed enters girt-water separation area, and water quality one is obtained after precipitating；
(2) water quality one enter pre-acidified area, intake it is quenched after obtain water quality two；
(3) water quality two enters level-one anaerobic zone, obtains water after carrying out the release of phosphorus and the fast breeding of active pollution index
Matter three；
(4) water quality three enters anoxic zone, and water quality four is obtained after being reacted；
(5) water quality four obtains water quality five after being reacted into main reaction region；
(6) water quality five enters settling zone, and settling zone obtains water quality six after carrying out mud-water separation to get purified regeneration is arrived
Water.
Based on the above-mentioned technical proposal it is found that sewage of the invention imitates self-purification system and method compared with the existing technology extremely
One of have the advantage that less:
1, denitrogenation dephosphorizing is high-efficient, TN (total nitrogen), TP (total phosphorus), COD removal rate respectively 90%, 99.5%, 93% with
On, water outlet TN, TP, COD concentration can be in 5mg/L, 0.05mg/L, 15mg/L or less；
2, without adding of agent, aeration energy consumption is lower than 0.09kW/t, and operating cost can be in 0.3 yuan/t hereinafter, water treatment procedure
In not because adding medicine generates additional carbon footprint；
3, it is suitable for low carbon-nitrogen ratio sewage, COD of sewage/TN ratio can still keep ideal denitrogenation dephosphorizing to imitate in 3-4 or so
Fruit；
4, for hypothermic phase denitrogenation dephosphorizing process excellent effect, it is 5-15 DEG C in temperature and is still able to maintain ideal denitrogenation dephosphorizing
Effect；
5, have effluent quality excellent, operating cost is low, and operational management is convenient, and without mating dosing pump etc., operational process can
All automation, application prospect are extensive.
Detailed description of the invention
Fig. 1 is the flow chart of deep purification of waste water method described in one embodiment of the invention；
Fig. 2 is showing when deep purification of waste water technology described in one embodiment of the invention designs realization by structure of reactor
It is intended to；
Fig. 3 is anti-when deep purification of waste water technology described in one embodiment of the invention is realized by reactor timing control
Answer structural schematic diagram；
Fig. 4 is Inlet and outlet water COD variation in the embodiment of the present invention 1；
Fig. 5 is Inlet and outlet water TN variation in the embodiment of the present invention 1；
Fig. 6 is Inlet and outlet water TP variation in the embodiment of the present invention 1.
In upper figure, appended drawing reference meaning is as follows:
1- water inlet；The desilting zone 2-；3- pre-acidified area；4- level-one anaerobic zone；The anoxic zone 5-；6- level-one aerobic zone；7- bis-
Grade anaerobic zone；8- second level aerobic zone；9- three-level anaerobic zone；10- three-level aerobic zone；11- level Four anaerobic zone；The reflux of 12- nitrification liquid
Flowmeter；13- sludge reflux flowmeter；14- nitrification liquid reflux pump；15- nitrification liquid return line；16- sludge reflux pipeline；
17- sludge reflux pump；18- supply air line；The settling zone 19-；20- residual sludge pump；21- bio-chemical effluent mouth；22- main reaction pond；
23- water decanter.
Specific embodiment
To make the objectives, technical solutions, and advantages of the present invention clearer, below in conjunction with specific embodiment, and reference
Attached drawing, the present invention is described in further detail.
During classical nitration denitrification, denitrogenation is mainly flowed back by nitrification liquid and is removed, but existing for this process
Problem is " ceiling " problem of denitrification percent, and denitrification zone nitrogen a part is the nitrate that nitrification liquid reflux comes, another
The ammonia nitrogen that part is brought into for water inlet, in traditional high load capacity denitrification process, ammonia nitrogen can not be removed in anoxic zone, hence into
Aerobic zone, being converted into after nitrate cannot still be removed, and still some cannot flow back into anoxic zone by nitrification liquid and be gone
It removes, causes the nitric efficiency of general sewage-treating reactor between 70-80%, it is difficult to have higher removal rate, in order to solve
This problem, can be by while keeping low dissolved oxygen, being the polysaccharide that microorganism accumulates in anoxic zone, PHA (poly- hydroxyl rouge
Fat acid esters) etc. organic matters, be unlikely to depleted in aerobic zone, so behind aerobic zone concatenated anaerobic zone as internal carbon source into
Row denitrification process makes biological denitrificaion break through tradition nitrification, the limitation of denitrification process ceiling.(anaerobic-aerobic-lacks AOA
Oxygen) reactor the problem of encountering sludge bulking caused by der Pilz during the experiment, this problem can pass through setting
Anaerobic zone, prehydrolysis acidification reduce settling zone load to control.
In Freshwater ecosystems, Riparian buffers are considered as the hot-zone of Anammox, a possible original among these
Because Riparian buffers exist, anaerobism, aerobic alternating, while the supply of its dissolved oxygen is in not abundant level again, this makes
Anaerobic ammonia oxidizing bacteria is enriched with, and can also pass through setting multistage micro- exposure during urban sewage treatment system reactor design
Gas, the aerobic zone and anaerobic zone of low dissolved oxygen are further enriched with anaerobic ammonia oxidizing bacteria to imitate this process.
A large amount of spoil disposals are considered as the method for operation for maintaining high-performance bio dephosphorization process that must keep, and which results in biologies to remove
The shorter sludge age of phosphorus, and generally require to maintain longer sludge age, this is considered as to be enriched with autotrophic bacterium in denitrification process
Mismatch during denitrogenation dephosphorizing on sludge age.But it in terms of the metabolic process of phosphorus, is calculated with conservation of matter, if in sludge
The concentration of phosphorus is increased to a higher level, then sludge age can be increased to higher state.Classical polyP bacteria is in ecological niche
In, it is given off energy by the hydrolysis of polyphosphate and absorbs extraneous small molecule volatile acid.In order to strengthen this process, pass through
Water inlet setting pre-acidified area converts volatile acid for the enrichment of polyP bacteria for a part of carbohydrate organic matter and improves sludge phosphorus
Concentration is of great significance.From the point of view of the limit of dephosphorization, it is considered that traditional denitrification dephosphorization system is only capable of arriving phosphorus ligands
1mg/L or so, but this numerical value is obtained under conditions of polyP bacteria is enriched with undesirable, if the ratio of polyP bacteria is increased to
Certain numerical value, the removal of phosphorus also will increase to higher level.
Sludge concentration is parameter important in sewage disposal system, in actual moving process in order to prevent on clarifier sludge
It is floating, the release of phosphorus, while guaranteeing the supply of dissolved oxygen, sludge concentration is often maintained at 3-6g/L, what this virtually increased accounts for
Ground.In order to reduce land occupation, sludge concentration can be further increased, since dissolved oxygen is lower, oxygen supply problem will not become limitation
Sexual factor, and clarifier sludge because denitrification float the problem of then can by reduce load, reduce internal carbon source content, reduce into
The nitrate content for entering sedimentation basin avoids sedimentation basin denitrification from excessively controlling Mud up-floating caused by denitrification.For phosphorus
Release problem, it should be noted that from the metabolic process of polyP bacteria, polyP bacteria can just be split only in the external world there are when volatile acid
Solution polyphosphate releases energy, and absorbs this part volatile acid, this is the rising of sedimentation basin phosphorus in macroscopical upper surface.And if heavy
Shallow lake pond does not have small molecule volatile acid, just should not there are problems that the release of phosphorus in sedimentation basin.For possible existing in operation
The accumulation of sedimentation basin small molecule volatile acid, reason are probably derived from spoil disposal unevenness, the long-term anaerobic processes in part caused by deposition
The small molecule volatile acid for leading to sludge anaerobic and releasing.Pass through a large amount of using largely of mechanical scraping and sucking machine now
This problem is avoided, meanwhile, if the volume die in sedimentation basin will further reduce using centripetal width sedimentation tank,
To avoid the problem that sedimentation basin phosphorus discharges.The promotion of the concentration of sludge can effectively reduce hydraulic detention time, further drop
Low capital construction cost and occupied area.
For pond depth problem, from the angle of aeration oxygen supply, the oxygen supply of 10m or less the depth of water and efficiency are very mature,
Land occupation can further be mitigated by the promotion of pond depth.
The capital expenditure of municipal sewage plant is in 3000 yuan/t water (daily treating capacity) at present, during this, operation
Cost at 0.6 yuan/t (containing aeration energy consumption and reagent cost), press 30 years by the depreciation time limit, and for depreciable cost in 0.27 yuan/t, operation is total
Cost is 0.87 yuan/t.Using long residence time, after underload sewage disposal system, cost of investment rises to 4000 yuan/t
Water (daily treating capacity), and due to the reduction of medicament and aeration energy consumption, operating cost can be reduced to 0.3 yuan/t, and depreciation period is still
By 30 years, depreciable cost at 0.36 yuan/ton, operation totle drilling cost in 0.66 yuan/t, relative to existing sewage treatment plant have at
This advantage., can be deep by increasing pond for occupied area problem, the measures such as the concentration of sludge solution is improved, this will be so that originally
Processing system has the advantage in operation relative to existing sewage disposal system.(contain from the carbon footprint of the full chain of sewage treatment
Medicament production) analysis, since this system is added without medicament, disposed of in its entirety system is more environmentally-friendly.
The invention discloses a kind of sewage to imitate self-purification system, comprising:
Level-one anaerobic zone which is provided with level-one anaerobic zone water inlet and level-one anaerobic zone water outlet；
Anoxic zone, which is provided with anoxic zone water inlet and anoxic zone water outlet and anoxic zone water inlet goes out with level-one anaerobic zone
Mouth of a river connection；
Main reaction region which is provided with main reaction region water inlet and main reaction region water outlet and main reaction region water inlet and anoxic
The connection of area's water outlet；And
Settling zone joins with settling zone water inlet and bio-chemical effluent mouth, settling zone water inlet and main reaction region water outlet thereon
It is logical.
Wherein, the purification system includes the girt-water separation area for precipitating inorganic particle, the girt-water separation Qu Shangshe
There are Disengagement zone water inlet and Disengagement zone water outlet, Disengagement zone water outlet is connect with level-one anaerobic zone water inlet.
Wherein, the pre-acidified area for quenched water inlet is equipped between the anaerobic zone and girt-water separation area.
Wherein, the main reaction region includes the concatenated main reaction region aerobic section of several grades and main reaction region anaerobism section or institute
The main reaction region stated includes main reaction pond；
Wherein, the main reaction region aerobic section is equipped with for providing the supply air line of oxygen；
Wherein, the nitrification liquid that anoxic zone is back to for nitrification liquid is equipped between the anoxic zone and main reaction region anaerobism section
Return line；
Wherein, the nitrification liquid return line is equipped with nitrification liquid reflux pump and nitrification liquid return flow meter.
Wherein, sludge reflux pipeline is equipped between the settling zone and level-one anaerobic zone；
Wherein, the mud return line road is equipped with sludge reflux pump；
Wherein, the settling zone is equipped with excess sludge discharge line, and excess sludge discharge line is equipped with excess sludge
Pump.
Wherein, the purification system includes filtering ponds, and the water inlet of filtering ponds and the water outlet of settling zone connect.
Wherein, the depth in each area of the purification system is 7-9m.
It is including as follows the invention also discloses a kind of purification method for carrying out sewage treatment using purification system as described above
Step:
(1) water quality to be processed enters girt-water separation area, and water quality one is obtained after precipitating；
(2) water quality one enter pre-acidified area, intake it is quenched after obtain water quality two；
(3) water quality two enters level-one anaerobic zone, obtains water after carrying out the release of phosphorus and the fast breeding of active pollution index
Matter three；
(4) water quality three enters anoxic zone, and water quality four is obtained after being reacted；
(5) water quality four obtains water quality five after being reacted into main reaction region；
(6) water quality five enters settling zone, and settling zone obtains water quality six after carrying out mud-water separation to get purified regeneration is arrived
Water.
Wherein, step (7) are also carried out after step (6):
(7) water quality six enters coagulating sedimentation area and multi-medium filtering pond, further removes oil removal and total phosphorus.
Wherein, filtering rate of the water quality six in multi-medium filtering pond described in step (7) is 2-5m/h；
Wherein, coagulation is not added in coagulating sedimentation area and multi-medium filtering pond in step (7) and help solidifying medicament, by mistake
Oil removal and total phosphorus are removed in retention during filter；Biomembrane is formed in filter material surface simultaneously, realizes synchronous nitration and denitrification process.
Wherein, water quality to be processed described in step (1) is 1-2h in girt-water separation area residence time；
Wherein, girt-water separation area bottom described in step (1) is rectangular pyramid；
Wherein, the compounded mix for constructing biomembrane hydrolysis acidification area is provided in step (2) in pre-acidified area；
Wherein, the compounded mix includes polyvinylidene chloride；
Wherein, the packing volume ratio of the compounded mix is 70-90%；
Wherein, the residence time in the level-one anaerobic zone of water quality two is 2-4h in step (3)；
Wherein, it is stirred during the fast breeding of the release of progress phosphorus and active pollution index in step (3)；
Wherein, reaction described in step (4) includes denitrifying phosphorus uptake reaction and Anammox reaction；
Wherein, the residence time 2-4h in the anoxic zone of water quality three in step (4)；
Wherein, step (4) stirs during the reaction；
Wherein, the nitrification liquid generated in step (5) flows back into anoxic zone, reflux ratio 100-400%；
Wherein, reaction described in step (5) includes one of step nitrification, anti-nitration reaction, multistage suction phosphorus reaction
Or the combination of a variety of reactions；
Wherein, main reaction region described in step (5) includes main reaction region aerobic section and main reaction region anaerobism section or described
Main reaction region include main reaction pond；
Wherein, the residence time in the main reaction region aerobic section of water quality four is 3-4h in step (5), and anoxic section stops
Time be 3-4h；
Wherein, submersible water impeller is laid in the main reaction region aerobic section simultaneously in step (5)；
Wherein, the concentration of dissolved oxygen is 0.1-0.5mg/L in main reaction region aerobic section section described in step (5)；
Wherein, the oxidation-reduction potential control of Electric potentials in afterbody main reaction region aerobic section section described in step (5)-
10-20mV；
Wherein, the ammonia nitrogen concentration generated in reaction step in step (5) is 2-4mg/L；
Wherein, sludge part obtained in mud-water separation step described in step (6) flows back into first order anaerobic zone；
Wherein, the sludge reflux generated in step (6) enters level-one anaerobic zone, reflux ratio 30-100%；
Wherein, the surface loading of settling zone described in step (6) is 0.3-0.8m/h；
Wherein, settling zone described in step (6) uses circumferential water feed peripheral effluent centripetal width flow pattern settling zone；
Wherein, in step (6) when the settling zone surface loading keeps 0.3-0.8m/h, in step (3)-step (7)
Sludge concentration be held in 6-15g/L；
Wherein, the total time that water quality stops in step (1)-(5) is 23-34h；
Wherein, step (4)-(6) can both be realized by the way that anoxic zone, anaerobic zone, aerobic zone etc. are arranged in reactor configuration,
It can also be controlled and be realized by the operation in timing in a pond body.
Wherein, when step (4)-(6) in timing control by realizing, nitrification liquid reflux is cancelled, and sedimentation basin is cancelled, and sludge returns
Stream starting point is moved from sedimentation basin to main reaction region rear end.When hydraulic retention when being realized on every section of runing time and configuration in timing
Between relationship be 20%-30% that runing time in step (4)-(6) timing is hydraulic detention time.
In one embodiment, the present invention is for example, by using following technical solution:
The present invention relates to deep under a kind of town sewage advanced purification system and method more particularly to C/N ratio or cryogenic conditions
Spend denitrogenation dephosphorizing.By extending biochemical section HRT to 23h-34h, the preposition compound pre-acidified area of filler increases small molecule volatile acid, exposes
Anoxic, aerobic strengthened denitrification are set after gas section, reduces settling zone surface loading and is removed to measures such as 0.3-0.8m/h for advanced nitrogen
Phosphorus provides the optimization on pool structure.In the method for operation, aerobic zone dissolved oxygen is controlled in 0.1-0.5mg/L, ORP current potential -10-
20mV keeps biochemistry pool water outlet ammonia nitrogen 2-4mg/L to control aeration quantity, promotes Nitrogen/Phosphorus Removal.It is arrived by improving sludge concentration
7-9m is arrived deeply to reduce land occupation in 6-15g/L, effective pond.Technology and method of the present invention, can be in influent COD/TN in 3.0-
4.0, at 5-12 DEG C of temperature, cooperation is filtered without medicament coagulating sedimentation, guarantee TN, TP, COD removal rate respectively 90%, 99.5%,
93% or more, while keeping aeration energy consumption lower than 0.09kW/t, have effluent quality excellent, operating cost is low, convenient for management etc. excellent
Gesture, application prospect are extensive.
In a preferred embodiment, the present invention is for example, by using following technical solution: a kind of imitative nature of town sewage is deep
Purification method is spent, in reactor configuration or the reactor method of operation:
(1) water inlet initially enters Disengagement zone 2 (girt-water separation area) by water inlet 1, setting pot is not removed inorganic
Particle precipitates, and prevents from impacting subsequent process；
(2) pre-acidified area 3 is set before level-one anaerobic zone 4, intakes quenched, converts volatilization for a part of organic matter
Acid；
(3) hydrolysis acidification water outlet enters level-one anaerobic zone 4, carries out the release of phosphorus in level-one anaerobic zone 4, while realizing activity
The fast breeding of sludge wadding body mitigates the growth of der Pilz, residence time 2-4h in level-one anaerobic zone 4；
(4) water outlet of level-one anaerobic zone 4 enters anoxic zone 5, and anoxic zone 5 is interior using nitrate as electron acceptor, carries out denitrification
Inhale phosphorus, the reaction such as Anammox；
(5) anoxic zone water outlet enters aerobic zone/anaerobic zone (main reaction region aerobic section and the main reaction of two-stage or thtee-stage shiplock
Area's anaerobism section) it is concatenated level-one aerobic zone 6, secondary anaerobic area 7, second level aerobic zone 8, three-level anaerobic zone 9, three in the present embodiment
Grade aerobic zone 10, level Four anaerobic zone 11 carry out the reaction of step nitrification and denitrification and multistage suction phosphorus reaction in these regions,
Ensure to be discharged phosphorus concentration to reach.
(6) water outlet of level Four anaerobic zone 11 enters settling zone 19, and mud-water separation, the reflux of sludge a part are carried out in settling zone 19
To level-one anaerobic zone 4, a part is discharged as excess sludge.
(7) water outlet of settling zone 19 enters coagulating sedimentation, and multi-medium filtering pond further removes SS, suspended state phosphorus, from biochemistry
Water outlet 21 is discharged, and finally realizes out water reuse (treatment.
Wherein, in step (1)-(7), pond body pond is deep in 7-9m, thus reduce occupied area, step (1)-(5) total water
The power residence time is in 23-34h；
Girt-water separation area in step (1), hydraulic detention time 1-2h, bottom are that tetragonous wimble structure connects sludge pump row
Silt；
Wherein, in step (2) pre-acidified area be arranged polyvinylidene chloride (Poly (vinylidene chloride),
PVDC) compounded mix, packing ratio 70-90% construct biomembrane hydrolysis acidification area；
Wherein, hydraulic detention time 2-4h in step (3), and be stirred, while sludge reflux enters anaerobic zone, it flows back
Compare 30%-100%；
Wherein, 5 hydraulic detention time 2-4h of anoxic zone in step (4), and be stirred, nitrification liquid flows back into anoxic
Area, reflux ratio 100-400%；
Wherein, anoxic zone described in step (5) enters two-stage or the reaction of three-level aerobic/anaerobic after completion of the reaction；It reacted
The every aerobic residence time 3-4h of level-one, anoxic zone residence time 3-4h in journey, while submersible water impeller, this reality are laid in aerobic zone
It applies and lays submersible water impeller in example using water decanter 23, be both to carry out plug-flow stirring in aerobic aeration, it is equal with ensure to react
Even property.
Wherein, aerobic zone dissolved oxygen concentration described in step (5) is 0.1-0.5mg/L, afterbody aerobic section ORP electricity
Position control is in -10-20mV, while remaining ammonia nitrogen concentration is in 2-4mg/L.
Wherein, settling zone surface loading described in step (6) uses circumferential water feed peripheral effluent in 0.3-0.8m/h, pond type
Individual sludge reflux pump is arranged in centripetal width stream settling zone, every pond.
Wherein, when settling zone surface loading keeps 0.3-0.8m/h, the sludge concentration in step (3)-(7) is kept
In 6-15g/L, to further increase load, occupied area is reduced.
Wherein, step (1)-(2) are designed by reactor configuration and are realized；Step (3)-(5) can both pass through reactor structure
Space in type, which is arranged, to be realized, can also be controlled and be realized by the operation in timing in a pond body, real in timing control
Now, nitrification liquid reflux is cancelled, and every section of runing time and the relationship of hydraulic detention time are step (3)-(5) in timing in timing
Its runing time is the 20%-30% of hydraulic detention time in steric configuration when upper realization.
Wherein, the filtering velocity in multi-medium filtering pond described in step (7) is 2-5m/h.
Wherein, coagulating sedimentation area and multi-medium filtering pond do not add coagulation and help solidifying medicament in step (7), by filtering
Retention removal SS and suspended state phosphorus in the process, while biomembrane is formed in filter material surface, synchronous nitration is realized under low dissolved oxygen
Denitrification process further realizes the removing of nitrogen, finally to realize deep purification of waste water.
Wherein, the main reaction region aerobic section is equipped with for providing the supply air line 18 of oxygen；
Wherein, the nitrification liquid that anoxic zone is back to for nitrification liquid is equipped between the anoxic zone and main reaction region anaerobism section
Return line 15；
Wherein, the nitrification liquid return line 15 is equipped with nitrification liquid reflux pump 14 and nitrification liquid return flow meter 12.
Wherein, sludge reflux pipeline 16 is equipped between the settling zone 19 and level-one anaerobic zone 4；
Wherein, the sludge reflux pipeline 16 is equipped with sludge reflux pump 17；
Wherein, the settling zone 19 is equipped with excess sludge discharge line, and excess sludge discharge line is equipped with remaining dirty
Dredge pump 20.
Wherein, (Fig. 2) is realized by reactor configuration (sewage imitates self-purification system) design in step (1)-(2)；Step
(3)-(5) can be both arranged by the space in reactor configuration to be realized, can also pass through the fortune in timing in a pond body
Row control is realized, when realizing in timing control (Fig. 3), nitrification liquid reflux is cancelled, and every section of runing time is stopped with waterpower in timing
It is hydraulic detention time in steric configuration that the relationship for staying the time, which is step (3)-(5) its runing time when realizing in timing,
20%-30%.
Explanation is further elaborated to technical solution of the present invention below by way of specific embodiment combination attached drawing.It should be noted that
, following specific embodiments are only as example, the scope of protection of the present invention is not limited thereto.
Chemicals used in following embodiments and raw material are commercially available gained or are made by oneself by well known preparation method
It obtains.
Embodiment 1
Using the imitative nature sewage treatment process of INSR of the present invention, (sewage imitates nature depth for Shandong sewage treatment plant
Purification method), 30,000 tons/d of water, the pond INSR total hrt 36h are handled, (such as by optimization design on structure of reactor
Shown in Fig. 2) it realizes, two-stage aerobic, anaerobism section strengthened denitrification are set after first order anoxic.Its influent COD in 180mg/L or so,
Intake total nitrogen 53mg/L or so, water inlet total phosphorus in 6mg/L or so, aerobic zone dissolved oxygen 0.1-0.8mg/L, sludge concentration 6g/L,
Settling zone surface loading 0.8m/h, settling zone water outlet directly filtering water outlet after coagulating sedimentation, is added without PAC, the medicaments such as PAM,
Winter low temperature phase operational effect is good, and ammonia nitrogen problem not up to standard is not present, and runs ton water consumption 0.18-0.30kW/t, fortune at present
Cost is relatively low for row.Ammonia nitrogen is discharged in 4mg/L or so to promote denitrogenation effect by control aerobic zone ORP and settling zone in operational process
Fruit.Conventional water outlet COD is discharged total nitrogen 6mg/L or so (as shown in Figure 5) 15mg/L or so (as shown in Figure 4), and water outlet total phosphorus exists
0.05mg/L or so (as shown in Figure 6) is discharged SS in 6mg/L or so.
Embodiment 2
Jiangsu sewage treatment plant using INSR of the present invention imitate nature sewage treatment process, processing 60,000 tons of water/
D realizes that reactor configuration such as (Fig. 3) is realized by the timing control that reactor is run, and carries out anoxic again after aerobic aeration and stirs
Strengthened denitrification effect is mixed, operation timing is water inlet stirring 1h, stirs denitrogenation 1h, is aerated 2h, denitrogenation 0.5h after stirring, precipitating
1h drains 0.5h.Biochemistry pool total hrt 26h, dissolved oxygen control is in its water inlet of 0.3-1.5mg/L in aeration process
COD is in 300mg/L or so, and total nitrogen 45mg/L or so of intaking, total phosphorus of intaking is in 5mg/L or so, sludge concentration 5g/L, winter low temperature
Phase does not find the low problem of nitric efficiency, runs ton water consumption 0.30-0.50kW/t at present, and operating cost is lower.Operational process
In by control aerobic zone ORP and water outlet ammonia nitrogen in 2mg/L or so to promote denitrification effect.Conventional total water outlet COD is in 30mg/L
Left and right, total to be discharged total nitrogen 5mg/L or so, total total phosphorus that is discharged is discharged SS in 7mg/L or so in 0.01mg/L or so.Operation at present
Ton water consumption 0.15-0.20kW/t.
Embodiment 3
Nature sewage treatment process is imitated using INSR of the present invention in district in Beijing rural sewage treatment station, handles water
It 50 tons/d, is realized by the optimization design in reactor configuration, reactor configuration is as shown in Fig. 2, water outlet is aspirated using ceramic membrane
It is discharged, two-stage aerobic, anaerobism section strengthened denitrification is set after first order anoxic.Its influent COD is in 160mg/L or so, total nitrogen of intaking
40mg/L or so, total phosphorus of intaking is in 3mg/L or so, and moisture film designs water flux 25L/m out2/ h runs ton water consumption at present
0.60-0.83kW/t.Denitrification effect is promoted in 0.5mg/ or so by control aerobic zone dissolved oxygen in operational process, sludge is dense
Spend 12g/L.Conventional water outlet COD is discharged total nitrogen 10mg/L or so (Fig. 5) at 35mg/L or so (Fig. 4), is discharged total phosphorus in 0.2mg/
L or so (Fig. 6) is discharged SS in 2mg/L or so.
Particular embodiments described above has carried out further in detail the purpose of the present invention, technical scheme and beneficial effects
Describe in detail bright, it should be understood that the above is only a specific embodiment of the present invention, is not intended to restrict the invention, it is all
Within the spirit and principles in the present invention, any modification, equivalent substitution, improvement and etc. done should be included in protection of the invention
Within the scope of.
Claims (10)
1. a kind of sewage imitates self-purification system characterized by comprising
Level-one anaerobic zone which is provided with level-one anaerobic zone water inlet and level-one anaerobic zone water outlet；
Anoxic zone which is provided with anoxic zone water inlet and anoxic zone water outlet and anoxic zone water inlet and level-one anaerobic zone water outlet
Connection；
Main reaction region, which is provided with main reaction region water inlet and main reaction region water outlet and main reaction region water inlet goes out with anoxic zone
Mouth of a river connection；And
Settling zone, thereon with settling zone water inlet and bio-chemical effluent mouth, settling zone water inlet and main reaction region water outlet connection.
2. purification system according to claim 1, which is characterized in that
The purification system includes the girt-water separation area for precipitating inorganic particle, the girt-water separation area be equipped with Disengagement zone into
The mouth of a river and Disengagement zone water outlet, Disengagement zone water outlet are connect with level-one anaerobic zone water inlet.
3. purification system according to claim 2, which is characterized in that
The pre-acidified area for quenched water inlet is equipped between the anaerobic zone and girt-water separation area.
4. purification system according to claim 1, which is characterized in that
The main reaction region includes that the concatenated main reaction region aerobic section of several grades and main reaction region anaerobism section or the master are anti-
Answering area includes main reaction pond；
Preferably, the main reaction region aerobic section is equipped with for providing the supply air line of oxygen；
Preferably, being equipped with the nitrification liquid for being back to anoxic zone for nitrification liquid between the anoxic zone and main reaction region anaerobism section
Return line；
As further preferred, the nitrification liquid return line is equipped with nitrification liquid reflux pump and nitrification liquid return flow meter.
5. purification system according to claim 1, which is characterized in that
Sludge reflux pipeline is equipped between the settling zone and level-one anaerobic zone；
Preferably, the mud return line road is equipped with sludge reflux pump；
Preferably, the settling zone is equipped with excess sludge discharge line, excess sludge discharge line is equipped with excess sludge
Pump.
6. purification system according to claim 1, which is characterized in that
The purification system includes filtering ponds, and the water inlet of filtering ponds and the water outlet of settling zone connect.
7. purification system according to claim 1, which is characterized in that
The depth in each area of purification system is 7-9m.
8. a kind of purification method for being carried out sewage treatment using the purification system as described in claim any one of 1-7, feature are existed
In including the following steps:
(1) water quality to be processed enters girt-water separation area, and water quality one is obtained after precipitating；
(2) water quality one enter pre-acidified area, intake it is quenched after obtain water quality two；
(3) water quality two enters level-one anaerobic zone, obtains water quality three after carrying out the release of phosphorus and the fast breeding of active pollution index；
(4) water quality three enters anoxic zone, and water quality four is obtained after being reacted；
(5) water quality four obtains water quality five after being reacted into main reaction region；
(6) water quality five enters settling zone, and settling zone obtains water quality six after carrying out mud-water separation to get purified recycled water is arrived.
9. purification method according to claim 8, which is characterized in that
It is also carried out after step (6) step (7):
(7) water quality six enters coagulating sedimentation area and multi-medium filtering pond, further removes oil removal and total phosphorus.
Preferably, filtering rate of the water quality six in multi-medium filtering pond described in step (7) is 2-5m/h；
Preferably, not adding coagulation in coagulating sedimentation area and multi-medium filtering pond in step (7) and helping solidifying medicament, by mistake
Oil removal and total phosphorus are removed in retention during filter；Biomembrane is formed in filter material surface simultaneously, realizes synchronous nitration and denitrification process.
10. the method for purification according to claim 8, which is characterized in that
Water quality to be processed described in step (1) is 1-2h in girt-water separation area residence time；
Preferably, girt-water separation area bottom described in step (1) is rectangular pyramid；
Preferably, the compounded mix for constructing biomembrane hydrolysis acidification area is provided in step (2) in pre-acidified area；
As further preferred, the compounded mix includes polyvinylidene chloride；
As further preferred, the packing volume ratio of the compounded mix is 70-90%；
Preferably, the residence time in the level-one anaerobic zone of water quality two is 2-4h in step (3)；
Preferably, being stirred during the fast breeding of the release of progress phosphorus and active pollution index in step (3)；
Preferably, reaction described in step (4) includes denitrifying phosphorus uptake reaction and Anammox reaction；
Preferably, the residence time 2-4h in the anoxic zone of water quality three in step (4)；
Preferably, step (4) stirs during the reaction；
Preferably, the nitrification liquid generated in step (5) flows back into anoxic zone, reflux ratio 100-400%；
Preferably, reaction described in step (5) includes one of step nitrification, anti-nitration reaction, multistage suction phosphorus reaction
Or the combination of a variety of reactions；
Preferably, main reaction region described in step (5) includes main reaction region aerobic section and main reaction region anaerobism section or described
Main reaction region include main reaction pond；
As further preferred, the residence time in the main reaction region aerobic section of water quality four is 3-4h, anoxic in step (5)
Section residence time is 3-4h；
As further preferred, submersible water impeller is laid in the main reaction region aerobic section simultaneously in step (5)；
As further preferred, the concentration of dissolved oxygen is 0.1-0.5mg/L in main reaction region aerobic section section described in step (5)；
As further preferred, in afterbody main reaction region aerobic section section described in step (5) oxidation-reduction potential current potential
Control is in -10-20mV；
Preferably, the ammonia nitrogen concentration generated in reaction step in step (5) is 2-4mg/L；
Preferably, sludge part obtained in mud-water separation step described in step (6) flows back into first order anaerobic zone；
Preferably, the sludge reflux generated in step (6) enters level-one anaerobic zone, reflux ratio 30-100%；
Preferably, the surface loading of settling zone described in step (6) is 0.3-0.8m/h；
Preferably, settling zone described in step (6) uses circumferential water feed peripheral effluent centripetal width flow pattern settling zone；
Preferably, in step (6) when the settling zone surface loading keeps 0.3-0.8m/h, in step (3)-step (7)
Sludge concentration be held in 6-15g/L；
Preferably, the total time that water quality stops in step (1)-step (5) is 23-34h；
Preferably, step (4)-step (6) both can be by being arranged anoxic zone, anaerobic zone, aerobic zone etc. in reactor configuration
It realizes, can also be controlled and be realized by the operation in timing in a pond body；
Preferably, nitrification liquid reflux is cancelled, and sedimentation basin is cancelled, dirty when step (4)-step (6) in timing control by realizing
Mud reflux starting point is moved from sedimentation basin to main reaction region rear end；Every section of runing time is stopped with waterpower when realizing on configuration in timing
The relationship for staying the time is 20%-30% that runing time in step (4)-(6) timing is hydraulic detention time.
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| CN114604970A (en) * | 2022-05-11 | 2022-06-10 | 北京博汇特环保科技股份有限公司 | Improved A2O biochemical reaction system and sewage treatment method |
| CN114804339A (en) * | 2022-04-19 | 2022-07-29 | 青岛思普润水处理股份有限公司 | BFM form-based efficient AOA coupling anaerobic ammonia oxidation sewage treatment method and system |
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