CN109020044A - Method for wastewater treatment and sludge reduction - Google Patents
Method for wastewater treatment and sludge reduction Download PDFInfo
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- CN109020044A CN109020044A CN201710427588.2A CN201710427588A CN109020044A CN 109020044 A CN109020044 A CN 109020044A CN 201710427588 A CN201710427588 A CN 201710427588A CN 109020044 A CN109020044 A CN 109020044A
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- sludge
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- wastewater treatment
- mud decrement
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- 239000010802 sludge Substances 0.000 title claims abstract description 118
- 238000000034 method Methods 0.000 title claims abstract description 53
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 33
- 230000009467 reduction Effects 0.000 title abstract description 3
- 239000002351 wastewater Substances 0.000 claims abstract description 52
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 26
- 230000015556 catabolic process Effects 0.000 claims abstract description 22
- 238000006731 degradation reaction Methods 0.000 claims abstract description 22
- 238000004062 sedimentation Methods 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 239000006228 supernatant Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000010992 reflux Methods 0.000 claims description 43
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 230000001376 precipitating effect Effects 0.000 claims description 16
- 239000004411 aluminium Substances 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 229920002401 polyacrylamide Polymers 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 238000005189 flocculation Methods 0.000 claims 1
- 230000016615 flocculation Effects 0.000 claims 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 19
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 19
- 239000011574 phosphorus Substances 0.000 abstract description 19
- 230000003647 oxidation Effects 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 11
- 239000010865 sewage Substances 0.000 abstract description 6
- 230000006037 cell lysis Effects 0.000 abstract 1
- 230000009469 supplementation Effects 0.000 abstract 1
- 238000012545 processing Methods 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 230000018044 dehydration Effects 0.000 description 9
- 238000006297 dehydration reaction Methods 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000012028 Fenton's reagent Substances 0.000 description 4
- 239000003945 anionic surfactant Substances 0.000 description 4
- MTAZNLWOLGHBHU-UHFFFAOYSA-N butadiene-styrene rubber Chemical compound C=CC=C.C=CC1=CC=CC=C1 MTAZNLWOLGHBHU-UHFFFAOYSA-N 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 3
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 description 3
- 230000009089 cytolysis Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 239000010452 phosphate Substances 0.000 description 3
- 230000032258 transport Effects 0.000 description 3
- 229920000459 Nitrile rubber Polymers 0.000 description 2
- 230000004308 accommodation Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 210000004027 cell Anatomy 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004094 surface-active agent Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 239000005955 Ferric phosphate Substances 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 229920000388 Polyphosphate Polymers 0.000 description 1
- 229920000037 Polyproline Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006701 autoxidation reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
- 239000001506 calcium phosphate Substances 0.000 description 1
- 235000011010 calcium phosphates Nutrition 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 210000000805 cytoplasm Anatomy 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 229940032958 ferric phosphate Drugs 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- -1 iron ion Chemical class 0.000 description 1
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 description 1
- 229910000399 iron(III) phosphate Inorganic materials 0.000 description 1
- 239000003446 ligand Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 230000032696 parturition Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000001205 polyphosphate Substances 0.000 description 1
- 235000011176 polyphosphates Nutrition 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 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
- 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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
- C02F11/08—Wet air oxidation
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/06—Sludge reduction, e.g. by lysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
-
- 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
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- 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
-
- 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
Landscapes
- 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)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Activated Sludge Processes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention provides a method for wastewater treatment and sludge reduction, and belongs to the field of sewage treatment. The invention combines Fenton oxidation and MBR process, and specifically comprises the following steps: 1) the wastewater to be treated enters a Fenton reactor for oxidation reaction; 2) the oxidized mixed liquid enters a sedimentation tank for separation, and the separated precipitated sludge is discharged into a sludge treatment system; the separated supernatant sequentially enters an A tank, an O tank and an MBR tank for biochemical degradation; 3) and part of activated sludge discharged from the MBR tank flows back to the tank A for supplementation, the rest of activated sludge is used as a residual sludge Fenton reactor, and MBR effluent is discharged out of the system. The process effectively solves the problems of long process flow, high cost, large sludge output and secondary pollution of the existing wastewater treatment process. In addition, the method performs mixed treatment on the excess sludge and the refractory wastewater in the Fenton reactor, and synchronously realizes cell lysis and wall breaking of the excess sludge, improvement of biochemical property of the refractory wastewater and removal of high-concentration phosphorus.
Description
Technical field
The invention belongs to sewage treatment fields, and in particular to a kind of group technology is while carrying out wastewater treatment, substantially
Reduce excess sludge production.Processing especially suitable for organic wastewater with difficult degradation thereby.
Background technique
In recent years, with the rapid development of the industries such as petrochemical industry, plastics, synthetic fibers, coking, printing and dyeing, it is various containing
The waste water of the organic pollutant of a large amount of difficult for biological degradation accordingly increases, they enter water body and cause serious pollution to environment.
This kind of wastewater toxicity is big, complex in composition, and chemical oxygen consumption (COC) is high, and biodegradability is poor, and general microorganism is hardly degraded effect to it
Fruit, therefore organic wastewater with difficult degradation thereby generally improves wastewater biodegradability using pretreatment, then enters back into biochemical treatment unit, root
According to processing requirement difference, it can also increase advanced treating.
Due to the lower price high efficiency of bioanalysis, becomes the core cell of wastewater treatment, but the generation of a large amount of excess sludges, make it
Processing cost accounts for the 25%~65% of sewage farm overall running cost.The processing modes such as traditional landfill, burning can be to ring
Secondary pollution is caused in border, thus while how to realize wastewater treatment excess sludge decrement, it has also become the project of extensive concern.
CN105417894A discloses a kind of high concentration, refractory wastewater method, using " pretreatment+biochemical degradation+
Post-processing " technique.Pretreatment uses " light electrolysis+Fenton+ Multifunctional waste water processor ", and biochemical degradation uses " A2/O+A/
O ", post-processing is using " biofilter+multi-medium filtering+biological activated carbon absorption ", and this method is applied widely, treatment effect
It is good.But process flow is very long, corresponding operation is complicated, operating cost is high；In addition a large amount of excess sludges generated are burned,
Secondary pollution can be generated.
CN202465460U discloses a kind of processing system for low-carbon-source micro polluted source difficult to degrade, uses
“Fenton+A2O+MBR " technique.Using the OH of strong oxidizing property, wastewater biodegradability is improved；Using the crown_interception of MBR film,
The removal effect for improving nitrogen phosphorus saves occupied area instead of secondary settling tank.The processing approach of the not clear excess sludge of the technique,
Provide only a kind of processing system of waste water.
CN101508513A discloses a kind of sludge decrement process of nitrogen phosphorus ligands in enhanced sewage, using " anaerobic hydrolysis+
MBR+ biochemistry dephosphorization+sludge lysis " technique.The biodegradability of waste water is improved by anaerobic hydrolysis, MBR strengthens nitrogen phosphorus and organic matter
Degradation efficiency, biochemical dephosphorization using polyP bacteria carry out anaerobic phosphorus release, using physics, chemistry or biotechnology carry out sludge it is molten
Born of the same parents realize mud decrement.The technique combines wastewater treatment and mud decrement, but phosphorus recycles in systems always without arranging
Unit out cannot degrade since phosphorus can only be shifted as inorganic salts, cause phosphorus concentration accumulation in system to increase, influence to be discharged water
The index of phosphorus in matter.
CN103896401A discloses water treatment facilities and the side of a kind of excess sludge reduction and strengthening biological carbon and phosphorous removal
Method, using " A2/ O-MBR+ microwave-alkali-H2O2" technique.Utilize " A2/ O-MBR " handles waste water, utilizes " microwave-alkali-H2O2" at
Excess sludge is managed, sludge yield is reduced.The technique connects wastewater treatment and Treatment of Sludge, it is contemplated that the processing of excess sludge
And the removal of phosphorus, but opposite process is longer, and it is at high cost.
Summary of the invention
The present invention in conjunction with MBR technique, provides Fenton oxidation to a kind of method of wastewater treatment and mud decrement, improves
The problem of existing sewage treatment technology process is long, costly, sludge yield is big, causes secondary pollution.
The method of a kind of wastewater treatment of the present invention and mud decrement, including the following steps:
1) waste water to be processed enters Fenton reactor progress oxidation reaction；
2) mixed liquor after aoxidizing enters sedimentation basin and is separated, and the precipitating sludge isolated is discharged into sludge treating system；
The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；
3) amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, remaining returns to Fenton as excess sludge
Reactor, MBR are discharged discharge system.
The method of wastewater treatment of the present invention and mud decrement, wherein adjust Fenton reactor pH value be 3~
7, preferably 3~4.
The method of wastewater treatment of the present invention and mud decrement, wherein the temperature of control Fenton reactor is 30
~60 DEG C, preferably 45~55 DEG C.
The method of wastewater treatment of the present invention and mud decrement, wherein the H in Fenton reactor2O2With Fe2+'s
Molar ratio is 10:1~0.5:1, preferably 3:1~1:1.
The method of wastewater treatment of the present invention and mud decrement, wherein waterpower of the waste water in Fenton reactor
Residence time is 5~120min, preferably 30~60min.
The method of wastewater treatment of the present invention and mud decrement, wherein the pH value for adjusting sedimentation basin is 6~9, preferably
It is 7~8.
The method of wastewater treatment of the present invention and mud decrement, wherein flocculant, the wadding are added in sedimentation basin
Solidifying agent is selected from one or more of poly-aluminium, Polyferric Sulfate, polyacrylamide, polysilicate.
The method of wastewater treatment of the present invention and mud decrement, wherein the pond O mixed liquid recycle ratio is 50%-
400%, preferably 100%~300%.
The method of wastewater treatment of the present invention and mud decrement, wherein the amount of activated sludge reflux of the pond MBR discharge
To the pond A, reflux ratio is 100%~400%.
The method of wastewater treatment of the present invention and mud decrement, wherein the amount of activated sludge reflux of the pond MBR discharge
To the pond A, reflux ratio is 200%~300%.
Fenton reactor of the present invention uses usual operating conditions, can be obtained by operation conditions optimization
More preferably treatment effect.
The pond A of the present invention, the pond O are respectively anaerobic pond and aerobic tank, and operating procedure condition is this field routine
Condition.
The strong oxidizing property OH that the method for the invention utilizes Fenton reagent fast reaction to generate, reacts with organic matter,
So that C-C key or c h bond is fissioned, larger molecular organics difficult to degrade are degraded to small molecule to improve giving birth to for waste water
The property changed；Then biochemical waste water enters A/O-MBR system, improves sludge concentration using the efficient crown_interception of film, strengthens drop
Solve efficiency.The present invention utilizes the crown_interception of MBR film to extend the activated sludge residence time simultaneously, and sludge is made to reach autoxidation drop
Solution, to reduce excess sludge production；The excess sludge that MBR system is periodically discharged is made by the oxidation of Fenton reagent
The cytoplasm of microorganism is cracked in sludge, and it is back to A/O-MBR system again in the form of organic substrate, is passed through
The further metabolism of microorganism reduces the purpose of sludge yield；The reflux of organic matter solves in biosystem use simultaneously
The problem of additional carbon, reduces the operating cost of whole set process.It, can be by the phosphorus in sludge with phosphate radical after sludge lysis broken wall
Form release, utilize iron ion in Fenton reagent to form ferric phosphate precipitating, processing system be discharged, guarantee water outlet phosphorus
It is up to standard.
Beneficial effects of the present invention:
The present invention, to excess sludge and used water difficult to degradate mixed processing, is produced in Fenton reactor using Fenton reagent
Raw strong oxidizing property OH, synchronizes the raising for realizing excess sludge lysis broken wall and used water difficult to degradate biochemical.Reduce land occupation
Area reduces investment and operating cost, upgrades conducive to the original position in sewage farm.
The present invention discharges after removing sludge broken wall using the metal ion generated in Fenton reaction process in sedimentation basin
Its impact to subsequent bio reaction system is effectively reduced in phosphate radical out.Utilize the phosphorus released in metal ion and sludge
Hydrochlorate generates the calcium phosphate precipitation of indissoluble, and the hydroxide that part is formed has flocculating effect, has Adsorption work to phosphate radical
With entire using the innoxious discharge of precipitating and the flocculated dual function form that precipitates the harmful phosphorus released in sludge
Processing system does not need additional Dephosphorization reagent, can reduce operating cost.
Detailed description of the invention
Fig. 1 is the method and process flow diagram of wastewater treatment of the present invention and mud decrement.
Specific embodiment
Elaborate below to the embodiment of the present invention: the present embodiment carries out under the premise of the technical scheme of the present invention
Implement, gives detailed embodiment and process, but protection scope of the present invention is not limited to following embodiments, following implementation
Test method without specific conditions in example, usually according to normal condition.
As shown in Figure 1,1) waste water to be processed enters Fenton reactor progress oxidation reaction, passes through and add acid-base accommodation pH
Value is 3~7, preferably 3~4；Reaction temperature control is 30~60 DEG C, preferably 45~55 DEG C；H2O2With Fe2+Molar ratio be
10:1~0.5:1, preferably 3:1~1:1；Hydraulic detention time of the waste water in oxidation reactor is 5~120min, preferably
30~60min.2) mixed liquor after Fenton reaction oxidation enters sedimentation basin and is separated, and passes through addition acid-base accommodation precipitating
The pH value in pond is 6~9, preferably 7~8；Flocculant can be added in sedimentation basin accelerates settling velocity, the precipitating sludge isolated
It is discharged into sludge treating system；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation.3) nitre in the pond O
Change liquid mass reflux ratio be 50%-400%, preferably 100%~300%；The amount of activated sludge reflux of the pond MBR discharge is to the pond A
It is supplemented, activated sludge mass reflux ratio is 100%~400%, preferably 200%~300%；Remaining as excess sludge into
Enter Fenton reactor and carries out oxidation broken wall；MBR is discharged discharge system.4) excess sludge and waste water to be processed of the pond MBR discharge
Into Fenton reactor, step 1) is repeated, realizes the purpose of wastewater treatment and mud decrement.
In above method step 2), the sludge treating system uses filters pressing or centrifuge separation.
In above method step 2), select plus flocculant can be poly-aluminium, Polyferric Sulfate, polyacrylamide, in polysilicate
The compound of one or more, preferably poly-aluminium and polyacrylamide.
Embodiment 1
Handle certain butadiene-styrene rubber phosphorus-containing wastewater, influent COD 1200mg/L, phosphorus 150mg/L.It is anti-that waste water enters Fenton
Device is answered to carry out oxidation reaction, H2O2With Fe2+Molar ratio be 2:1, pH value in reaction 3.2, reaction temperature be 50 DEG C, hydraulic retention
Time is 60min；It is 7.3 that mixed liquor after oxidation, which adjusts pH value, enters sedimentation basin separation, the precipitating isolated after poly-aluminium is added
Sludge transports outward landfill after passing through centrifugal dehydration；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；O
Nitrification liquid mass reflux ratio in pond is 150%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, and activity is dirty
Mud mass reflux ratio is 200%；Remaining enters Fenton reactor as excess sludge.It is 45mg/L that MBR, which is discharged COD, and phosphorus is
0.3mg/L；Sludge yield is every m3Waste water 4.3kg (moisture content 80%, similarly hereinafter).
Comparative example 1
COD is 1200mg/L, and phosphorus is certain butadiene-styrene rubber phosphorus-containing wastewater of 150mg/L, carries out oxygen into Fenton reactor
Change reaction, H2O2With Fe2+Molar ratio be 2:1, pH value in reaction 3.2, reaction temperature is 50 DEG C, and hydraulic detention time is
60min；It is 7.3 that mixed liquor after oxidation, which adjusts pH value, enters sedimentation basin separation after poly-aluminium is added, the precipitating sludge isolated is logical
Landfill is transported outward after crossing centrifugal dehydration；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；In the pond O
Nitrification liquid mass reflux ratio is 150%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, activated sludge quality
Reflux ratio is 200%；After remaining is discharged into sludge concentrating pot concentration as excess sludge, into sludge dewatering equipment processing.MBR water outlet
COD is 67mg/L, phosphorus 1.5mg/L；Sludge yield is every m3Waste water 6.6kg.
Embodiment 2
Handle the without phosphorus waste water of certain butadiene-styrene rubber, influent COD 900mg/L.Waste water enters Fenton reactor and is aoxidized
Reaction, H2O2With Fe2+Molar ratio be 3:1, pH value in reaction 4.5, reaction temperature be 45 DEG C, hydraulic detention time 40min；
After mixed liquor adjusting pH value after oxidation is 6.5, separated into sedimentation basin, the precipitating sludge isolated passes through outside after centrifugal dehydration
Fortune landfill；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；Nitrification liquid mass reflux in the pond O
Than being 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, and activated sludge mass reflux ratio is 400%；
Remaining enters Fenton reactor as excess sludge.It is 48mg/L that MBR, which is discharged COD, and sludge yield is every m3Waste water 0.75kg.
Comparative example 2
COD is the without phosphorus waste water of certain butadiene-styrene rubber of 900mg/L, carries out oxidation reaction, H into Fenton reactor2O2With
Fe2+Molar ratio be 3:1, pH value in reaction 4.5, reaction temperature be 45 DEG C, hydraulic detention time 40min；It is mixed after oxidation
It closes liquid and adjusts after pH value is 6.5 and enter sedimentation basin separation, the precipitating sludge isolated enters sludge concentrating pot；Supernatant enters
A2/ O carries out biochemical degradation, and water outlet enters secondary settling tank, and secondary clarifier effluent COD is 98mg/L；Sedimentation in secondary sedimentation tank sludge enters sludge
Concentration tank processing, is filled by transporting outward after centrifugal dehydration, and sludge yield is every m3Waste water 1.25kg.
Embodiment 3
Handle certain surface active agent wastewater, influent COD 2900mg/L, anionic surfactant 2600mg/L.It is useless
Water enters Fenton reactor and carries out oxidation reaction, H2O2With Fe2+Molar ratio be 3:1, pH value in reaction 3.5, reaction temperature
It is 40 DEG C, hydraulic detention time 120min；It is 8.2 that mixed liquor after oxidation, which adjusts pH value, is entered after adding polyacrylamide
Sedimentation basin separation, the precipitating sludge isolated transport outward landfill after passing through filter-press dehydration；The supernatant isolated sequentially enters the pond A, O
Pond and the pond MBR carry out biochemical degradation；Nitrification liquid mass reflux ratio in the pond O is 100%；The amount of activated sludge of the pond MBR discharge
It is back to the pond A to be supplemented, activated sludge mass reflux ratio is 300%；Remaining enters Fenton reactor as excess sludge.
It is 56mg/L that MBR, which is discharged COD, and anionic surfactant 3.2mg/L, sludge yield is every m3Waste water 0.9kg.
Comparative example 3
COD is 2900mg/L, and anionic surfactant is certain surface active agent wastewater of 2600mg/L, micro- into iron carbon
Electrolysis cells are handled, and wherein pH value control adds the control of iron charcoal weight ratio in 2:1, hydraulic detention time is 3.0
30min；Water outlet enters Fenton reactor and carries out oxidation reaction, H2O2With Fe2+Molar ratio be 6:1, pH value in reaction 4.5,
Reaction temperature is 40 DEG C, hydraulic detention time 120min；Mixed liquor after oxidation adjusts after pH value is 8.5 and carries out precipitating point
From precipitating sludge enters sludge concentrating pot；Supernatant enters A/O and carries out biochemical degradation, and water outlet enters secondary settling tank, secondary clarifier effluent
COD is 65mg/L, anionic surfactant 6.3mg/L；Sedimentation in secondary sedimentation tank sludge enters sludge concentrating pot processing, passes through plate
Landfill is transported outward after frame filter-press dehydration, sludge yield is every m3Waste water 1.8kg.
Embodiment 4
Certain coking wastewater, influent COD 3900mg/L are handled, waste water enters Fenton reactor and carries out oxidation reaction, H2O2
With Fe2+Molar ratio be 1:2, pH value in reaction 4.0, reaction temperature be 30 DEG C, hydraulic detention time 120min；After oxidation
It is 8.3 that mixed liquor, which adjusts pH value, is added according to sedimentation basin separation is entered after silicate, the precipitating sludge isolated passes through filter-press dehydration
Outward transport landfill afterwards；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；Nitrification liquid quality in the pond O
Reflux ratio is 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, and activated sludge mass reflux ratio is
350%；Remaining enters Fenton reactor as excess sludge.It is 60mg/L that MBR, which is discharged COD, and sludge yield is every m3Waste water
0.9kg。
Comparative example 4
COD is certain coking wastewater of 3900mg/L, sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation.In the pond O
Nitrification liquid mass reflux ratio is 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, activated sludge quality
Reflux ratio is 350%；After remaining is discharged into sludge concentrating pot concentration as excess sludge, into sludge dewatering equipment processing.MBR water outlet
COD is 116mg/L, and sludge yield is every m3Waste water 1.5kg.
Embodiment 5
Certain coking wastewater, influent COD 4500mg/L are handled, waste water enters Fenton reactor and carries out oxidation reaction, H2O2
With Fe2+Molar ratio be 1:1, pH value in reaction 3.0, reaction temperature be 55 DEG C, hydraulic detention time 120min；After oxidation
It is 6.6 that mixed liquor, which adjusts pH value, enters sedimentation basin separation after Polyferric Sulfate is added, the precipitating sludge isolated passes through outside after filter-press dehydration
Fortune landfill；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；Nitrification liquid mass reflux in the pond O
Than being 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, and activated sludge mass reflux ratio is 350%；
Remaining enters Fenton reactor as excess sludge.It is 72mg/L that MBR, which is discharged COD, and sludge yield is every m3Waste water 1.5kg.
Comparative example 5
COD is certain coking wastewater of 4500mg/L, sequentially enters the pond A and the pond O and carries out biochemical degradation, it is heavy that water outlet enters two
Pond.Nitrification liquid mass reflux ratio in the pond O is 200%；Amount of activated sludge reflux to the pond A of secondary settling tank discharge is supplemented,
Activated sludge mass reflux ratio is 350%；After remaining is discharged into sludge concentrating pot concentration as excess sludge, at sludge dewatering equipment
Reason.Secondary clarifier effluent COD is 135mg/L, and sludge yield is every m3Waste water 2.1kg.
Embodiment 6
Certain nitrile rubber waste water, influent COD 800mg/L are handled, waste water enters Fenton reactor and carries out oxidation reaction,
H2O2With Fe2+Molar ratio be 8:1, pH value in reaction 3.5, reaction temperature be 35 DEG C, hydraulic detention time 30min；Oxidation
It is 8.8 that mixed liquor afterwards, which adjusts pH value, enters sedimentation basin separation after adding polyacrylamide, the precipitating sludge isolated passes through pressure
Landfill is transported outward after filter dehydration；The supernatant isolated sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；Nitrification in the pond O
Liquid mass reflux ratio is 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, activated sludge mass reflux
Than being 300%；Remaining enters Fenton reactor as excess sludge.It is 45mg/L that MBR, which is discharged COD, and sludge yield is every m3
Waste water 0.5kg.
Comparative example 6
Influent COD is certain nitrile rubber waste water of 800mg/L, sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation.O
Nitrification liquid mass reflux ratio in pond is 200%；Amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, and activity is dirty
Mud mass reflux ratio is 350%；After remaining is discharged into sludge concentrating pot concentration as excess sludge, into sludge dewatering equipment processing.MBR
Water outlet COD is 56mg/L, and sludge yield is every m3Waste water 0.8kg.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
Various corresponding changes and modifications, but these corresponding changes and modifications can be made according to the present invention by knowing those skilled in the art
It all should belong to the protection scope of the claims in the present invention.
Claims (10)
1. a kind of method of wastewater treatment and mud decrement, which is characterized in that this method including the following steps:
1) waste water to be processed enters Fenton reactor progress oxidation reaction；
2) mixed liquor after aoxidizing enters sedimentation basin and is separated, and the precipitating sludge isolated is discharged into sludge treating system；Separation
Supernatant out sequentially enters the pond A, the pond O and the pond MBR and carries out biochemical degradation；
3) amount of activated sludge reflux to the pond A of the pond MBR discharge is supplemented, remaining returns to Fenton reaction as excess sludge
Device, MBR are discharged discharge system.
2. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that adjust Fenton reactor
PH value is 3~7, preferably 3~4.
3. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that control Fenton reactor
Temperature is 30~60 DEG C, preferably 45~55 DEG C.
4. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that the H in Fenton reactor2O2
With Fe2+Molar ratio be 10:1~0.5:1, preferably 3:1~1:1.
5. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that waste water is in Fenton reactor
In hydraulic detention time be 5~120min, preferably 30~60min.
6. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that the pH value for adjusting sedimentation basin is 6
~9, preferably 7~8.
7. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that add flocculation in sedimentation basin
Agent, the flocculant are selected from one or more of poly-aluminium, Polyferric Sulfate, polyacrylamide, polysilicate.
8. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that the pond O mixed liquid recycle ratio is
50%-400%, preferably 100%~300%.
9. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that the pond MBR is discharged amount of activated
For sludge reflux to the pond A, reflux ratio is 100%~400%.
10. the method for wastewater treatment as described in claim 1 and mud decrement, it is characterised in that the part of the pond MBR discharge is living
Property sludge reflux to the pond A, reflux ratio is 200%~300%.
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Application publication date: 20181218 |