CN106277314B - A kind of biochemistry denitrogenation dephosphorizing sewage disposal system and method - Google Patents
A kind of biochemistry denitrogenation dephosphorizing sewage disposal system and method Download PDFInfo
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- CN106277314B CN106277314B CN201610622667.4A CN201610622667A CN106277314B CN 106277314 B CN106277314 B CN 106277314B CN 201610622667 A CN201610622667 A CN 201610622667A CN 106277314 B CN106277314 B CN 106277314B
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- 239000010865 sewage Substances 0.000 title claims abstract description 101
- 238000000034 method Methods 0.000 title claims abstract description 63
- 239000010802 sludge Substances 0.000 claims abstract description 159
- 230000020477 pH reduction Effects 0.000 claims abstract description 69
- 230000007062 hydrolysis Effects 0.000 claims abstract description 68
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 67
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 47
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 47
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000000126 substance Substances 0.000 claims abstract description 28
- 238000010992 reflux Methods 0.000 claims abstract description 20
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 9
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 25
- 229910052698 phosphorus Inorganic materials 0.000 claims description 25
- 239000011574 phosphorus Substances 0.000 claims description 25
- 230000008569 process Effects 0.000 claims description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 238000009826 distribution Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 11
- 241000894006 Bacteria Species 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 229920000388 Polyphosphate Polymers 0.000 claims description 7
- 229920000037 Polyproline Polymers 0.000 claims description 7
- 230000029087 digestion Effects 0.000 claims description 7
- 239000001205 polyphosphate Substances 0.000 claims description 7
- 235000011176 polyphosphates Nutrition 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 239000003344 environmental pollutant Substances 0.000 claims description 6
- 231100000719 pollutant Toxicity 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 238000004659 sterilization and disinfection Methods 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 238000005255 carburizing Methods 0.000 claims description 3
- 239000011790 ferrous sulphate Substances 0.000 claims description 3
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 3
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 3
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims description 3
- 239000000654 additive Substances 0.000 claims description 2
- 230000000996 additive effect Effects 0.000 claims description 2
- 238000005273 aeration Methods 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 239000003814 drug Substances 0.000 abstract description 4
- 230000008859 change Effects 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 238000005276 aerator Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000006396 nitration reaction Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002574 poison Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000003042 antagnostic effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000479 mixture part Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- DJFBJKSMACBYBD-UHFFFAOYSA-N phosphane;hydrate Chemical compound O.P DJFBJKSMACBYBD-UHFFFAOYSA-N 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
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- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Health & Medical Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Toxicology (AREA)
- Molecular Biology (AREA)
- Microbiology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The present invention relates to sewage treatment fields, more particularly to a kind of biochemistry denitrogenation dephosphorizing sewage disposal system and method, the system includes up-flow hydrolysis acidification Sludge Bed, biological carbon and phosphorous removal device, device for separating mud and water and the chlorination equipment being successively connected with the outlet of sewer of up-flow hydrolysis acidification Sludge Bed；It is provided on the device for separating mud and water for by the sludge reflux pipeline of isolated sludge reflux to up-flow hydrolysis acidification Sludge Bed and/or the biological carbon and phosphorous removal device；Adding or even not adding for carbon source, Dephosphorization reagent and other medicaments can be reduced using the system, biological sludge yield and chemical sludge yield can be reduced, the three big irreconcilable contradictions occurred during biological carbon and phosphorous removal fully effective can be solved, efficiency, the reliability and stability of denitrogenation dephosphorizing are improved.
Description
Technical field
The present invention relates to sewage treatment field more particularly to a kind of biochemistry denitrogenation dephosphorizing sewage disposal system and sides
Method.
Background technique
The severization trend of Chinese sewage drainage standard becomes clear day by day, in November, 2015, and Environmental Protection Department issues " cities and towns
Wastewater Treatment discharge standard " (exposure draft), and Beijing and Tianjin have taken the lead in implementing stringent place mark
It is quasi-.The characteristics of due to Chinese cities and towns sewage, in the case where not additional carbon, total nitrogen is difficult the method row up to standard by biology
It puts, the method dephosphorization qualified discharge with biology can not be look to.
Currently used Biological Nitrogen Removal Processe has AAO, SBR, EH-BFB Biological Nitrogen Removal Processe, UCT and VIP method
Deng and its deformation.
Wherein, AAO process flow is as shown in Fig. 5.
" Code for design of outdoor sewerage engineering " (GB50014): " when needing denitrogenation dephosphorizing simultaneously, anaerobic/anoxic/good is preferably used
Oxygen method (AAO method, also known as A2O method) ".Sewage can achieve while remove organic followed by anaerobism section, anoxic section and aerobic section
The purpose of object and denitrogenation dephosphorizing.
Inverted AAO process process is as shown in Fig. 6.
The main distinction of inverted AAO process process and AAO technique is that anaerobic zone and anoxic zone position change.
UCT process flow is as shown in Fig. 7.
UCT method is similar to AAO method, and mainly by two o'clock difference, returnedactivatedsludge is back to anoxic zone, anoxic zone mixed liquor
It is back to anaerobic zone.It is additionally arranged an anoxic zone in UCT deformation, is additionally arranged reflux of the aerobic zone to the second anoxic zone.
VIP process flow is as shown in Fig. 8.
VIP method is similar to UCT method and AAO method, but return-flow system usage is different.
It is as shown in Fig. 9 that EH-BFB biochemical denitrification dephosphorization technique sets process flow.
EH-BFB biochemical denitrification dephosphorization technique sets technique main feature, uses pressure water distributor and carries out to hydrolysis acidification pool
Water distribution uniformity, to form bulking sludge bed；Aerobic unit has added partial filler, so as to form aerobic fluidized bed；Sludge
Return-flow system usage is changed.
The biological denitrification phosphorous removal technique being currently known is required to solve three big irreconcilable contradictions: 1, sludge age length demand
The problem of differing greatly；2, because there are nitrate in anaerobic zone that asking for denitrification and anaerobic phosphorus release occurs simultaneously for returned sludge
Topic；3, phosphorus and denitrification are released using easily biodegradable organics as carbon source, there is because carbon source it is insufficient caused by competitive contradiction.Its
In, AAO can not solve " 1,2,3 ", and inversion A AO can not be solved " 1 ", and UCT and VIP can not solve " 1,3 ", EH-BFB biochemical denitrification
Dephosphorization technique, which sets technique, can not solve " 2,3 ".EH-BFB biochemical denitrification dephosphorization technique sets technique using pure bioanalysis dephosphorization, is containing
When phosphorus concentration is higher, requires supplementation with carbon source just and can ensure that water outlet phosphorus content qualified discharge.It is larger while needing to examine to generate sludge quantity
Consider the problem of releasing phosphorus in sludge subsequent processes.
Other techniques are all made of biological treatment+chemical dephosphorization mode and carry out dephosphorization, chemical flocculation area total inflow >=
The inflow that biochemical unit starts, chemical flocculation Qu always intake in phosphorus content≤raw water phosphorus content, and need to consider sludge
The problem of phosphorus is released in subsequent processes, therefore Dephosphorization reagent dosage is big during entire denitrogenation dephosphorizing, generates a large amount of remaining
Sludge.
Current all denitrification dephosphorization techniques make the sludge of aerobic generation drain into Treatment of Sludge list directly as excess sludge
Member, therefore the carbon source in sewage could not be fully used, and in the insufficient situation of carbon source, need to add more carbon sources.
Therefore, a kind of denitrification dephosphorization technique meaning for adding less or even not adding carbon source, Dephosphorization reagent and other medicaments is studied
Justice is great far-reaching.
Summary of the invention
The purpose of the present invention is in view of the defects existing in the prior art and insufficient, it is dirty to provide a kind of biochemistry denitrogenation dephosphorizing
Water treatment system specifically adopts the following technical scheme that
A kind of biochemistry denitrogenation dephosphorizing sewage disposal system, including up-flow hydrolysis acidification Sludge Bed, successively with it is described
The outlet of sewer of up-flow hydrolysis acidification Sludge Bed connected biological carbon and phosphorous removal device, device for separating mud and water and chlorination equipment；
It is provided on the device for separating mud and water for by isolated sludge reflux to the up-flow hydrolysis acidification
The sludge reflux pipeline of Sludge Bed and/or the biological carbon and phosphorous removal device.
Wherein, up-flow hydrolysis acidification Sludge Bed of the present invention is a kind of change of existing reactor for hydrolysis and acidification
Shape, structure is similar in " reactor for hydrolysis and acidification sewage treatment project technical specification " (HJ2047), including bed body (shape
Can be cylinder, can also be cuboid), the bottom of bed body is provided with sewage inlet, active sludge in bed body, top
It is provided with the weir plate and effluent trough for collecting water outlet, up-flow hydrolysis acidification Sludge Bed of the invention and existing reactor
Difference, which is only that in bed body, to be provided with for returned sludge to be imported the intracorporal entrance of bed.The present invention is artificially by the up-flow
The inside of hydrolysis acidification Sludge Bed is divided into three parts, respectively lower part, middle part and top from bottom to top, and the height of each section accounts for about
The 1/3 of entire bed height.Up-flow hydrolysis acidification Sludge Bed of the present invention have distinct functional areas: lower part and
The major function of central region is the anaerobic digestion of the hydrolysis acidification and hydrolyzing sludge residue of sewage；Distance away from bottom accounts for bed body
The major function in region is the removal of NO3-N and NO2-N in returned sludge between total height about 2/3~5/6；Away from bottom away from
It is anaerobic phosphorus release from the major function for accounting for region between bed body total height about 5/6~liquid level.
Biological carbon and phosphorous removal device of the present invention also contains specific functional areas, includes but are not limited to aerobic zone,
Anoxic zone, anaerobic zone, the processing unit well known in the art such as film area, the present invention is to the specific layout of each functional areas and reflux
Mode is not done specifically limited, and the layout and reflux type of several functional areas can use it is known in the art that as in background technique
The AAO layout type referred to, inversion A AO layout type, basic phase can be achieved in UTC layout type or VIP layout type etc.
Same function.The layout type of currently preferred biological carbon and phosphorous removal device is AAO formula or MSBR formula.
In a kind of specific embodiment, the biological carbon and phosphorous removal device includes sequentially connected anaerobic pond, anoxic
Pond and aerobic tank, the aerobic tank are equipped with the interior return line for the mud mixture of aerobic tank to be back to anoxic pond.
In another specific embodiment, the biological carbon and phosphorous removal device includes sequentially connected anoxic pond, detests
Oxygen pond and aerobic tank are again provided with the pipeline for the mud mixture of aerobic tank to be back to anoxic pond on the aerobic tank.
In any one of the above embodiment, in order to ensure going on smoothly for aerobic tank reaction, biological carbon and phosphorous removal dress
Setting further includes blast aerator for being passed through from air to the aerobic tank.Blast aerator, which is known in the art, to be set
It is standby, commercially available acquisition.
Preferably, which further includes chemical dephosphorization pond, the sewage inlet in the chemical dephosphorization pond with it is described
The outlet of sewer of up-flow hydrolysis acidification Sludge Bed is connected, the outlet of sewer and the biological carbon and phosphorous removal in the chemical dephosphorization pond
The sewage inlet of device is connected.
The present invention carries out chemical dephosphorization to sewage by effluent mode, and pure biological phosphate-eliminating in the prior art or is being
Compared with the chemical dephosphorization (easily forming dephosphorization with the antagonistic relations of sludge sludge age) that section carries out before, during and after system, effluent mode of the invention
There is no the problems that sludge age length demand difference is larger.In addition, the treating capacity of the dephosphorization process only accounts for the 10- of sewage treatment total amount
30%, therefore cost of investment is low, occupied area is small.
Preferably, the distance away from its bottom accounts for the flat of bed body total height 2/3 inside the up-flow hydrolysis acidification Sludge Bed
The returned sludge distribution head for distributing returned sludge is provided on face；The up-flow hydrolysis acidification Sludge Bed bottom and/or
It is evenly equipped with the sewage distribution head for distributing treatment sewage.
Preferably, which further includes the fluid distributor for being respectively used to distribution treatment sewage and returned sludge, described
Device well known in the art can be used in fluid distributor, such as valve regulated distributor, perforated pipe water distributor, jet flow water distributor, number
Control rotational flow distributor, weir notch etc..
The water outlet of the fluid distributor is one-to-one by pipeline with sewage distribution head and returned sludge distribution head respectively
Connection, the fluid distributor can uniformly, continuous, stable allocation fluid.
The present invention does not do particular determination to the structure of device for separating mud and water, such as MBR well known in the art (film life can be used
Object reactor), the specific equipment such as biological rotating disk or " secondary settling tank+V-type filter tank " is discharged, SS by device for separating mud and water
(suspended solid content) is able to satisfy water outlet and requires.
The present invention does not also do particular determination to the structure of chlorination equipment, for example, disinfection by ultraviolet light can be used, sodium hypochlorite disappears
Poison or ozonization keep excrement colibacillus group number in water outlet up to standard.
Sewage treatment is carried out using any one of the above sewage disposal system a second object of the present invention is to provide a kind of
Method, this method comprises the following steps:
(1) treatment sewage is passed through to the bottom of the up-flow hydrolysis acidification Sludge Bed, sewage moves from bottom to top,
During by sludge area, pollutant therein occurs hydrolysis acidification with anaerobic sludge and reacts, and then rises to up-flow water
The top of solution acidification bed is collected to effluent trough and enters biological carbon and phosphorous removal device, bottom excess sludge after weir plate collects water outlet
It is discharged into sludge treatment equipment；
(2) sewage in biological carbon and phosphorous removal device after denitrogenation dephosphorizing, into device for separating mud and water；
(3) into the mud mixture of device for separating mud and water after mud-water separation, sludge flows back via sludge reflux pipeline
To up-flow hydrolysis acidification Sludge Bed sludge area and/or biological carbon and phosphorous removal device, the sterilized device disinfection in water body part is laggard
Enter device for recycling sewage.
In a kind of specific embodiment, denitrogenation dephosphorizing described in step (2) specifically comprises the following steps:
S201: sewage enters anaerobic pond, and the polyP bacteria in anaerobic pond sufficiently releases phosphorus in anaerobic pond, after releasing phosphorus
Activated sludge with mix into sewage therein after into anoxic zone；
S202: the denitrifying bacterium in anoxic pond makes the NO3-N and NO2-N in sewage be reduced to nitrogen, passes through
Sewage after anti-nitration reaction enters aerobic tank；
S203: in aerobic tank, the pollutant in sewage is by carburizing reagent and/or digestion reaction and/or aerobic phosphorus absorption
Reaction is further eliminated, and phosphorus is absorbed by polyP bacteria, and mineralized nitrogen is NO3-N and NO2-N；By the muddy water of aerobic tank
Mixture part is back to anaerobic pond, partially enters device for separating mud and water.
Preferably, in step (3), isolated sludge both can all be back to up-flow hydrolysis acidification Sludge Bed,
It can also be partly refluxed to up-flow hydrolysis acidification Sludge Bed, biological carbon and phosphorous removal device is partly refluxed to and (is such as back to biology
Initial position-anaerobic pond of denitrification dephosphorization apparatus).Since the water quality and quantity of sewage plant is larger with season and time fluctuation, lead to
Crossing can be can improve the removal rate of pollutant under the premise of up to standard to biological carbon and phosphorous removal device refluxing portion.
Isolated sludge is preferably all back to the sludge area of up-flow hydrolysis acidification Sludge Bed by the present invention.It is such
In the case of, returned sludge is thoroughly mixed to form mud mixture with the sewage after hydrolysis acidification reacts, and mud mixture is uniform
During by up-flow hydrolysis acidification Sludge Bed top (by distance about away from bed body bottom level about 2/3~5/6 it
Between), the nitrate in returned sludge is removed by a series of biological respinses, and the polyP bacteria in returned sludge is in an anaerobic environment
Release phosphorus；Excess sludge passes through hydrolysis, generates a large amount of degradable carbon sources, residue is by up-flow hydrolysis acidification Sludge Bed
It is further resolved during portion and lower part, final excess sludge generates small point of a large amount of degradable carbon sources, phosphate and ammonia etc.
Sub- substance, residue are discharged into sludge treatment equipment with base sludge.Returned sludge of the invention there are independent anti-nitration reaction area,
Therefore it thoroughly solves in existing biological denitrification phosphorous removal technique, the nitrate in returned sludge occurs anti-simultaneously in anaerobic zone
The problem of nitrification and anaerobic phosphorus release.Meanwhile although denitrification and anaerobic phosphorus release using degradable organic matter as carbon source, by
In the problem of denitrification and anaerobic phosphorus release occurs simultaneously in anaerobic zone is not present, so also there is no competing caused by carbon source deficiency
Striving property contradiction, thus, it can realize in the insufficient situation of carbon source and add or even do not add carbon source less.
All excess sludges of the present invention pass through in the middle part of up-flow hydrolysis acidification Sludge Bed and the anaerobic digestion of lower part, reason
By upper, residual active sludge yield is lower than the prior art.Since up-flow hydrolysis acidification Sludge Bed continuum micromeehanics have sludge increasing
Long, sewage sludge SS changes out, and the sludge concentration of different parts is not identical, and SS is to change in returned sludge and water inlet, therefore
The sludge abatement amount of returned sludge can not be directly measured, but can be inferred that returned sludge in up-flow water with the following method
Solve the anaerobic digestion amount under the effect of acidification sludge bed.The method specifically:
(1) three parts of hydrolysis acidification sludge 500mL are taken to be fitted into the mineral water bottle of volume 1000L, sample is labeled as sample
1, sample 2 and sample 3.Two parts of returned sludge 500mL are taken to be respectively charged into the mineral water bottle of volume 1000L (labeled as sample
4) and in sample 2.With bottle cap sealing sample 1, sample 2, sample 3 and sample 4.
(2) sludge concentration for measuring sample 3 is 12g/L, returned sludge concentration 7g/L.
(3) sample 1 and sample 2 are rocked daily, rocks time 1min/L, static 1h, which loosens bottle cap, keeps bottle interior and environment
Continue to tighten bottle cap after pressure is equal.
(4) sample 1 and the sludge concentration of sample 2 are measured after 20d is respectively 10g/L, 7g/L.
(5) it calculates:
Returned sludge reduces at least 40% through anaerobic digestion 20d, sludge quantity as known from the above.Therefore residue of the invention is living
Property sludge yield than other techniques reduce 40% or more.
It is back to up-flow hydrolysis acidification Sludge Bed via pipeline through the isolated sludge of device for separating mud and water, so that dirty
Mud is flowed out in bed intracorporal extended residence time 0.5-1.5h, and from the outlet of sewer on up-flow hydrolysis acidification Sludge Bed top
It is mud mixture (its concentration be about returned sludge concentration 50%), therefore, whole sludge concentration is relatively uniform in system,
Mean sludge concentration is higher by 10% or more than the concentration of general hydrolysis acidification technique.
Preferably, the processing method further includes by the 10-30% in the sewage after acidified hydrolysis process in step (1)
The step of (percentage by volume) imports chemical dephosphorization pond and carries out chemical dephosphorization, and the sewage after dephosphorization is then imported anaerobic pond.Into
Preferably, the chemical dephosphorization uses ferrous sulfate dephosphorization agent, additive amount 1-3mg/L to one step.
In the prior art, the inflow of other process chemistry dephosphorization units >=total water inlet, Dephosphorization reagent dosage and dephosphorization
Molar ratio is generally 2~10:1, and dosage is 20mg/L × total water inlet under normal circumstances.Chemical dephosphorization unit inflow of the present invention
10~30% about always to intake, Dephosphorization reagent dosage and dephosphorization molar ratio are generally 1:1, and dosage is under normal circumstances
10mg/L × total water inlet × (10~30%), i.e., about 1~3mg/L × total water inlet.So chemical sludge output is other techniques
1/20~1/50, with the few advantage of sludge yield.
Preferably, the upflow velocity of sewage is 0.5-2m/h, top flow velocity of the sewage in up-flow hydrolysis acidification Sludge Bed
For 1.5-3m/h.
Preferably, sewage is 4-6h in the residence time of up-flow hydrolysis acidification Sludge Bed,
Preferably, residence time of the sewage in biological carbon and phosphorous removal device is 10-15h, wherein in anaerobic pond, anoxic
The residence time of pond and aerobic tank ratio is 1:(1-3): (4-8).
In a kind of specific embodiment, controlling residence time of the sewage in biological carbon and phosphorous removal device is 10h,
In, it is respectively 1h, 2h and 7h in the residence time of anaerobic pond, anoxic pond and aerobic tank.
It is further preferred that blasting air into aerobic tank using blast aerator, gas-water ratio is (6-8): 1.
Using system and method for the present invention, it can be achieved that being discharged continuous-stable qualified discharge, and in sewage treatment
Cheng Zhong can reduce adding or even not adding for carbon source, Dephosphorization reagent and other medicaments, can reduce biological sludge yield and change
Sludge yield is learned, the three big irreconcilable contradictions occurred during biological carbon and phosphorous removal fully effective can be solved, improve denitrogenation
Efficiency, the reliability and stability of dephosphorization.
Detailed description of the invention
Fig. 1 is the schematic diagram of sewage disposal system of the present invention；
Fig. 2 is a kind of concrete form of biological denitrification dephosphorization apparatus；
Fig. 3 is another concrete form of biological denitrification dephosphorization apparatus；
Fig. 4 is the structural schematic diagram of up-flow hydrolysis acidification Sludge Bed；
Fig. 5 is AAO process flow chart；
Fig. 6 is inverted AAO process flow chart；
Fig. 7 is UCT process flow chart；
Fig. 8 is VIP process flow chart；
Fig. 9 is EH-BFB biochemical denitrification dephosphorization technique process flow chart.
1, up-flow hydrolysis acidification Sludge Bed；101, activated sludge area；102, reflux sludge tube；103, water inlet pipe；104,
Outlet pipe；105, sewage pipe；2, biological carbon and phosphorous removal device；3, device for separating mud and water；4, chlorination equipment；5, blast aeration fills
It sets；6, chemical dephosphorization device；7, sludge treatment equipment；8, device for recycling sewage；9, sludge reflux pipeline；10, interior return line；
201, anaerobic pond；202, anoxic pond；203, aerobic tank.
Specific embodiment
The following examples are used to illustrate the present invention, but are not intended to limit the scope of the present invention..
Embodiment 1
A kind of sewage disposal system, as described in Figure 1, the sewage disposal system include up-flow hydrolysis acidification Sludge Bed 1, are risen
The structure of streaming hydrolysis acidification Sludge Bed 1 is specifically shown in Fig. 4, is filled with activated sludge area 101 in bed body, and reflux sludge tube 102
At pond body 2/3, water inlet pipe 103 is located at bed body bottom, and outlet pipe 104 is located at top, and sewage pipe 105 is located at lower part.
Further include the biological carbon and phosphorous removal device 2 being successively connected with the outlet pipe 104 of up-flow hydrolysis acidification Sludge Bed 1,
Device for separating mud and water 3 and chlorination equipment 4；
It is provided on the device for separating mud and water 3 for by isolated sludge reflux to the up-flow hydrolysis acidification
The sludge reflux pipeline 9 of Sludge Bed 1 and/or the biological carbon and phosphorous removal device 2.
Wherein, the structure of the biological carbon and phosphorous removal device 2 is as shown in Fig. 2, including sequentially connected anaerobic pond 201, lacking
Oxygen pond 202 and aerobic tank 203, and the interior reflux for sewage mixture to be back to anaerobic pond 201 is provided on aerobic tank 203
Pipeline 10.
The excess sludge being discharged from up-flow hydrolysis acidification Sludge Bed 1 enters sludge treatment equipment 7 through sewage pipe 105, disappears
Sewage qualified discharge or entrance device for recycling sewage 8 after poison recycle.
Embodiment 2
The difference of a kind of sewage disposal system, the system and embodiment 1 is only that: biological carbon and phosphorous removal apparatus structure is not
Together, the specific structure is shown in FIG. 3 for the embodiment biological carbon and phosphorous removal device, including sequentially connected anoxic pond 202, anaerobic pond
201 and aerobic tank 203, and the interior return line for sewage mixture to be back to anaerobic pond 201 is provided on aerobic tank 203
10。
Embodiment 3
A kind of sewage disposal system, the system are the further improvements made on the basis of embodiment 1, specifically: also
Including chemical dephosphorization device 6, the sewage inlet and the outlet of sewer phase of up-flow hydrolysis acidification Sludge Bed 1 of chemical dephosphorization device 6
Even, the outlet of sewer of chemical dephosphorization device 6 is connected with the sewage inlet of anaerobic pond 201.
By up-flow hydrolysis acidification Sludge Bed treated part water outlet enter the dephosphorization of chemical dephosphorization device after be passed through again
Anaerobic pond 201.
Embodiment 4
A kind of sewage disposal system, the system are the further improvements made on the basis of embodiment 1 or 2, specifically:
The inside of up-flow hydrolysis acidification Sludge Bed 1 accounts for about away from the distance of its bottom is provided with reflux in the plane of bed body total height 2/3
Distribution of sludge head, the bottom of up-flow hydrolysis acidification Sludge Bed 1 are evenly arranged with sewage distribution head, returned sludge distribution head and dirt
The moisture leftover of bolt of cloth is one-to-one connected with the fluid discharge pipe of corresponding fluid distributor through piping respectively.
Embodiment 5
A kind of sewage water treatment method is carried out using the system of embodiment 4, is included the following steps:
(1) treatment sewage is evenly distributed by fluid distributor to the bottom of the up-flow hydrolysis acidification Sludge Bed
Portion, sewage move from bottom to top, during passing through the bottom and middle part of up-flow hydrolysis acidification Sludge Bed, pollution therein
Object occurs hydrolysis acidification with the anaerobic sludge for being located at the region and reacts, and then rises to the top of up-flow hydrolysis acidification bed, passes through
Weir plate collects water outlet, into effluent trough, flows into anaerobic pond, bottom excess sludge is discharged into sludge treatment equipment；
(2) polyP bacteria being located in anaerobic pond sufficiently releases phosphorus in anaerobic pond, activated sludge and entrance after releasing phosphorus
Enter anoxic zone after sewage mixing therein；
(3) denitrifying bacterium being located in anoxic pond makes the NO3-N and NO2-N in sewage be reduced to nitrogen, by anti-
Sewage after nitration reaction enters aerobic tank；
(4) in aerobic tank, the pollutant in sewage is anti-by carburizing reagent and/or digestion reaction and/or aerobic phosphorus absorption
It should further be eliminated, phosphorus is absorbed by polyP bacteria, and mineralized nitrogen is NO3-N and NO2-N；It is mixed by the muddy water of aerobic tank
Polymer portion is back to anaerobic pond, partially enters device for separating mud and water；
(5) into the mud mixture of device for separating mud and water after mud-water separation, sludge flows back via sludge reflux pipeline
To fluid distributor, distribute via fluid distributor to up-flow hydrolysis acidification Sludge Bed, the sterilized device disinfection in water body part
Enter device for recycling sewage afterwards.
In the embodiment, upflow velocity of the sewage in up-flow hydrolysis acidification Sludge Bed bottom is 0.9m/h, top flow velocity
For 1.7m/h, sewage is 5h in the bed intracorporal residence time, is 1h in the anaerobic pond residence time, and the anoxic pond residence time is 2h,
The aerobic tank residence time is 7h, and the returned sludge of device for separating mud and water is all back to up-flow hydrolysis acidification Sludge Bed top.
Sewage quantity into chemical dephosphorization device accounts for the 20% of total amount, and chemical dephosphorization medicament is ferrous sulfate, injected volume 10mg/L.
(above each numerical value is mean value)
The related data that detection obtains up-flow hydrolysis acidification Sludge Bed is as follows: base sludge concentration mean value 15g/L, middle part
Sludge concentration mean value 12g/L, top sludge concentration mean value 10g/L, water outlet phosphorus content mean value is about 20mg/L.
Sewage described in the present embodiment is city domestic sewage, after above-mentioned processing, the Inlet and outlet water of city domestic sewage
Water standard is as shown in table 1, and water outlet reaches level-one A standard:
1 city domestic sewage Inlet and outlet water water standard (mg/L) of table
Note: Con trolling index when the outer numerical value of bracket is 12 DEG C of water temperature >, control when numerical value is water temperature≤12 DEG C in bracket
Index.
Although above having used general explanation, specific embodiment and test, the present invention is made to retouch in detail
It states, but on the basis of the present invention, it can be made some modifications or improvements, this is apparent to those skilled in the art
's.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, belong to claimed
Range.
Claims (3)
1. a kind of method of sewage treatment, which is characterized in that be carried out using biochemistry denitrogenation dephosphorizing sewage disposal system, institute
Stating sewage disposal system includes up-flow hydrolysis acidification Sludge Bed, and successively the sewage with the up-flow hydrolysis acidification Sludge Bed goes out
Mouth connected biological carbon and phosphorous removal device, device for separating mud and water and chlorination equipment；
It is provided on the device for separating mud and water for by isolated sludge reflux to the up-flow hydrolysis acidification sludge
The sludge reflux pipeline of bed；The distance away from its bottom accounts for bed body total height 2/3 inside the up-flow hydrolysis acidification Sludge Bed
The returned sludge distribution head for distributing returned sludge is provided in plane；The up-flow hydrolysis acidification Sludge Bed bottom is uniformly distributed
There is the sewage distribution head for distributing treatment sewage；It further include the fluid for being respectively used to distribution treatment sewage and returned sludge
Distributor；The water outlet of the fluid distributor passes through pipeline a pair with the sewage distribution head and returned sludge distribution head respectively
One connection；
The biological carbon and phosphorous removal device includes sequentially connected anaerobic pond, anoxic pond and aerobic tank；Alternatively, including being sequentially connected with
Anoxic pond, anaerobic pond and aerobic tank；It is equipped on the aerobic tank of each biological carbon and phosphorous removal device for will be aerobic
The mud mixture in pond is back to the interior return line of anoxic pond；It further include the blast aeration for being passed through air into aerobic tank
Device；
The sewage disposal system further includes chemical dephosphorization pond, and the sewage inlet and the up-flow in the chemical dephosphorization pond hydrolyze
The outlet of sewer of acidification sludge bed is connected, the sewage of the outlet of sewer in the chemical dephosphorization pond and the biological carbon and phosphorous removal device
Entrance is connected；
The sewage water treatment method includes the following steps:
(1) treatment sewage is passed through to the bottom of the up-flow hydrolysis acidification Sludge Bed, sewage moves from bottom to top, passing through
During the bottom and middle part of up-flow hydrolysis acidification Sludge Bed, pollutant therein is sent out with the anaerobic sludge for being located at the region
Unboiled water solution acidification reaction, then rises to the top of up-flow hydrolysis acidification bed, after weir plate collects water outlet, is collected to effluent trough
Into biological carbon and phosphorous removal device, bottom excess sludge is discharged into sludge treatment equipment；The upflow velocity of the sewage is 0.5-
2m/h, sewage are 1.5-3m/h in the top flow velocity of up-flow hydrolysis acidification Sludge Bed；The sewage is in up-flow hydrolysis acidification
The residence time of Sludge Bed is 4~6h；
(2) sewage in biochemistry denitrification dephosphorization apparatus after denitrogenation dephosphorizing, into device for separating mud and water；
(3) sludge in device for separating mud and water after mud-water separation is back to up-flow hydrolysis acidification dirt via sludge reflux pipeline
Mud bed, discharge or reuse after the sterilized device disinfection of water body after separation；
Wherein, denitrogenation dephosphorizing described in step (2) specifically comprises the following steps:
S201: the sewage after hydrolysis acidification enters anaerobic pond, and the polyP bacteria in anaerobic pond sufficiently releases phosphorus in anaerobic pond,
Activated sludge after releasing phosphorus enters anoxic zone after mixing with entrance sewage therein；
S202: the denitrifying bacterium in anoxic pond makes the NO3-N and NO2-N in sewage be reduced to nitrogen, by anti-nitre
Sewage after changing reaction enters aerobic tank；
S203: in aerobic tank, the pollutant in sewage is by carburizing reagent and/or digestion reaction and/or aerobic phosphorus absorption reaction
It is further eliminated, phosphorus is absorbed by polyP bacteria, and mineralized nitrogen is NO3-N and NO2-N；It is mixed by the muddy water of aerobic tank
Object part is back to anaerobic pond, partially enters device for separating mud and water；
Residence time of the sewage in biological carbon and phosphorous removal device is 10-15h, wherein in anaerobic pond, anoxic pond and aerobic
The residence time ratio in pond is 1:(1-3): (4-8).
2. processing method according to claim 1, which is characterized in that further include by acidified hydrolysis process in step (1)
10-30% in sewage afterwards imports chemical dephosphorization pond and carries out chemical dephosphorization, and the sewage after dephosphorization is then imported biological denitrificaion
The step of dephosphorization apparatus.
3. processing method according to claim 2, which is characterized in that the chemical dephosphorization uses ferrous sulfate dephosphorization agent,
Its additive amount is 1-3mg/L.
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