CN103130379B - Treatment method of coking ammonia distillation wastewater - Google Patents
Treatment method of coking ammonia distillation wastewater Download PDFInfo
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- CN103130379B CN103130379B CN201110400207.4A CN201110400207A CN103130379B CN 103130379 B CN103130379 B CN 103130379B CN 201110400207 A CN201110400207 A CN 201110400207A CN 103130379 B CN103130379 B CN 103130379B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 96
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 48
- 238000004939 coking Methods 0.000 title claims abstract description 22
- 238000004821 distillation Methods 0.000 title abstract 3
- 239000012528 membrane Substances 0.000 claims abstract description 30
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
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- 238000001802 infusion Methods 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 6
- 239000010865 sewage Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 3
- 239000000701 coagulant Substances 0.000 claims description 3
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 3
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 3
- 239000011790 ferrous sulphate Substances 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
- 239000007787 solid Substances 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 239000003929 acidic solution Substances 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 10
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 2
- 238000004062 sedimentation Methods 0.000 abstract description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 239000002894 chemical waste Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 5
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 3
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000011368 organic material Substances 0.000 description 3
- 150000003384 small molecules Chemical class 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 2
- 241000976983 Anoxia Species 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 206010021143 Hypoxia Diseases 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 2
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 2
- 230000007953 anoxia Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000005518 electrochemistry Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
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- 229920002521 macromolecule Polymers 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
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- 238000006396 nitration reaction Methods 0.000 description 2
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- 238000005728 strengthening Methods 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
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- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- -1 hydroxyl radical free radical Chemical class 0.000 description 1
- 150000002475 indoles Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
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- 231100001234 toxic pollutant Toxicity 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a method for treating coking ammonia distillation wastewater, which comprises the following steps of pretreatment and biochemical treatment of the ammonia distillation wastewater, wherein the pretreatment adopts a regulating tank, an internal electrolysis reactor, a Fenton oxidation tank and a coagulating sedimentation tank, the biochemical treatment adopts a sequencing batch membrane bioreactor process, and the four steps of inflow, idling, reaction and discharge are carried out in sequence according to a time period; the method can effectively remove the organic pollutants and ammonia nitrogen which are difficult to degrade and enhance the quality of the effluent, and simultaneously reduce the operation and investment cost of equipment.
Description
Technical field
The invention belongs to water-treatment technology field, particularly relate to a kind for the treatment of process of coking distilled ammonia wastewater.
Background technology
Metallurgy industry is the super rich and influential family of China's disposal of pollutants, and one of coking chemical waste water source of pollution that to be metallurgy industry maximum.Except containing except a large amount of volatile phenols, COD, prussiate, sulfide in coking chemical waste water, also have the ammonia nitrogen of high density and the condensed-nuclei aromatics of many difficult degradations and heterogeneous ring compound, as indoles, naphthalene, quinoline etc., very big on the impact of environment, be considered to one of the most unmanageable trade effluent, for a long time, be the difficult problem that national each smelter bid is tackled key problems always.In recent years, along with the development of China's steel industry, the coking scale matched with it constantly expands, and consequent coking chemical waste water quantity discharged is multiplied, and pollution intensity is aggravated increasingly.
New by looking into, retrieve some relevant patent and articles, as " treatment process of coking chemical waste water " (CN 101781067) invention, this kind of method required process structures are more, and complex process, floor space is large, and running cost is also higher." a kind of process is except the method for the coking chemical waste water after ammonia " (CN 101875526A) invention, the method sludge volume is comparatively large, produce sludge handling problem, and ammonia nitrogen removal effect is undesirable." integral type film biological reactor Treatment of Wastewater in Coking " (Pei Liang etc.), this article discusses the feasibility by integral type film biological reactor Treatment of Wastewater in Coking, by Adjustment Tests operating parameters, to COD, NH
3-N and turbidity all achieve good treatment effect, but it is comparatively large to there is sludge volume, produce sludge handling problem, and ammonia nitrogen removal effect is undesirable.
Present Domestic generally adopts pre-treatment to add the second-stage treatment technique of biochemical treatment to the process of coking chemical waste water, but the pollutents such as the COD in conventional two stage biological processed waste water and ammonia nitrogen are all difficult to qualified discharge, can not meet new sewage drainage standard, seriously govern the development of enterprise.And before secondary biochemical treatment, abroad take the water quality that more complicated pre-treatment and additive method control enter biochemical system, prevent toxic pollutant excessive concentration, and after biochemical treatment flow process, take three grades of purification systems.So-called tertiary treatment is the technical process of the multiple physico-chemical process composition centered by biological treatment taking the compositions such as dephenolize, ammonia still process, biological treatment and activated carbon adsorption.But the operation of tertiary treatment process and investment cost are all higher, if filter out suitable pretreatment technology, make it after pre-treatment, greatly reduce the content entering the poisonous factor of secondary biochemical system, improve the biodegradability of waste water, in addition the efficient biochemical treatment system of follow-up employing, intensive treatment effluent quality, replaces tertiary treatment process with high costs with this, and the Sustainable development for enterprise has important practical significance.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art, the invention provides the treatment process of a kind of low cost, efficiently coking distilled ammonia wastewater, pre-treatment+efficient biochemical the process of distilled ammonia wastewater after optimizing, effectively removing Persistent organic pollutants and ammonia nitrogen, strengthening effluent quality while, operation and the investment cost of equipment can be reduced.
A treatment process for coking distilled ammonia wastewater, the method equipment used comprises equalizing tank, Inner electrolysis reactor, Fenton oxidation pond, coagulative precipitation tank and sequencing batch membrane bioreactor, and described method is undertaken by following operation:
A: the pre-treatment of distilled ammonia wastewater.First carry out pre-treatment to distilled ammonia wastewater, the distilled ammonia wastewater collected is passed into equalizing tank, add acid and regulate its pH value, the pH controlling waste water, between 2.6 ~ 3.1, becomes acidic solution, to be satisfied with the requirement of Inner electrolysis reaction; Waste water enters the top of Inner electrolysis reactor by infusion, carries out Inner electrolysis reaction.This technique take activated carbon granule as negative electrode, iron filings are anode, ionogen electric action forms the organic substance that galvanic cell processes comparatively easily degraded in waste water, under the combined action of the processes such as the reductive action of corrosion electrochemistry effect, iron, the throwing out of ironic hydroxide and the attached collection of electrochemistry, make organism generation oxidizing reaction, destroy its organic polymer structure.Keep the residence time of waste water in Inner electrolysis reactor to be 0.5-2.5h, water outlet flows into Fenton oxidation pond;
Fenton oxidation pond is batch operation, under the state constantly stirred, adds acid (being generally the vitriol oil), makes its pH value control between 2.8-3.2; Add ferrous sulfate solid subsequently, make the concentration of ferrous ion reach 100-300ppm, and then add the hydrogen peroxide solution that concentration is 900-1100ppm.Utilize H
2o
2at Fe
2+katalysis under produce and there is the hydroxyl radical free radical of very high oxidation potential, without organism remaining in the oxidized waste water selected.Under the state stirred, the controlled oxidization reaction times is 0.5-2h, and reacted waste water flows into coagulative precipitation tank;
Adding alkali lye in coagulative precipitation tank regulates the pH of waste water between 9-10, adds the coagulant aids PAM of 1ppm, stirs and staticly settle 25-40min after five minutes.After precipitation, the supernatant liquor of gained is pretreated distilled ammonia wastewater.
B: the biochemical treatment of distilled ammonia wastewater.Adopt sequencing batch membrane bioreactor technique (SBMBR), aerobic nitrification and anoxic denitrification environment is controlled by adopting the mode of stirring/aeration, temporally the cycle experiences inflow, idle, reaction, discharge four operations in turn to make whole system, seed sludge wherein in sequencing batch membrane bioreactor takes from the aerobic returned sluge in chemical plant, first put it in membrane bioreactor and tame one month, make sludge concentration reach 9500mg/L.
Flow into operation: pretreated distilled ammonia wastewater enters the bottom of membrane bioreactor by infusion, the reaction tank flowing into membrane bioreactor is sprayed through water distributor, by continuous stirring, mud is fully contacted with distilled ammonia wastewater, it is 1.5-2.5h that control anoxic enters the distilled ammonia wastewater time, and distilled ammonia wastewater pH controls at 8.5-9.0.By water inlet anoxia stirring, the high NH in water inlet can be utilized on the one hand
3the feature of-N, high COD, abundant carbon source is provided in reactor, carbon-nitrogen ratio is made substantially to meet Denitrification Conditions, nitrate-nitrogen reduction is made to become nitrogen, on the other hand, anoxia stirring is run has ring opening to organism such as the polycyclic aromatic hydrocarbons of some difficult degradations, it is easily degraded, namely improves the biodegradability of distilled ammonia wastewater.
Idle operation: period scope is 4-5h, and the active sludge microorganism now in reactor remains the environment of anoxic, can make full use of into water high-enriched organics as denitrifying carbon source, what anti-nitration reaction was carried out is more fully thorough.
Reaction process: start gas blower and start to carry out aeration to sewage, for the active sludge in membrane bioreactor provides sufficient oxygen, make it be in oxygen condition, it effectively can be degraded to the carbonaceous organic material in sewage.Meanwhile, the ammonium oxidation in waste water is become nitrite nitrogen and nitrate nitrogen by nitrifier, for anoxic phases provides sufficient electron acceptor(EA).Aerated reaction time controling controls between 7.5-8.5 at 15-17h, pH, aeration rate: flooding quantity (air water throughput ratio) controls at 25-35:1.Gas blower stops aeration, and reaction process terminates.
Discharge operation: under the negative pressure-pumping of suction pump or the effect of head difference, water and part small-molecule substance are through membrane module, become system water outlet through outlet pipeline, macromolecular substance, active sludge microorganism and inorganic particle are membrane module and are trapped in reactor.Discharge activity time controls as 1.5-2.5h, and quantity discharged controls, for partial discharge, after discharge operation terminates, to close suction pump, start the circulation of next cycle.
System repeats inflow in turn, leaves unused, reacts, discharges four operations within the time subsequently, whole system is in anoxic, the aerobic state replaced all the time, intermittent water inflow and water outlet, and in reaction process latter stage via shore pipe and the remaining active sludge of mud valve periodic exhaustion.
The invention has the beneficial effects as follows: provide one by equalizing tank, Inner electrolysis, Fenton oxidation and coagulating sedimentation combination process as pre-treatment, sequencing batch membrane bioreactor is as the method for biochemical section Treatment of Wastewater in Coking.High concentration coking is after process of the present invention, and effluent quality can reach Iron And Steel Industry water pollutions first discharge standard, and the tandem greatly increasing coking chemical waste water uses and recycle.Pretreated combination process can not only long-chain and cyclic organic materials in degrading waste water, and effectively can improve wastewater biodegradability, for follow-up process lays a good foundation.Biochemical section adopts sequencing batch membrane bioreactor, not only remain that conventional SBR technique capacity of resisting impact load is strong, oxygen transfer efficiency and biochemical reaction efficiency high, run relatively stable, not easily there is the advantages such as sludge bulking, and just can nitrification and denitrification be realized in single reactor, save anaerobic pond, anoxic pond, settling tank and return-flow system, greatly reduce technique floor space.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of coking distilled ammonia wastewater of the present invention process.
Embodiment
Below in conjunction with Fig. 1, the specific embodiment of the present invention is described further:
Distilled ammonia wastewater through the pretreatment process of equalizing tank, Inner electrolysis reactor, Fenton oxidation pond and coagulative precipitation tank, makes most of refractory organic compounds be degraded to small-molecule substance successively, improves the biodegradability of distilled ammonia wastewater; Pretreated distilled ammonia wastewater enters in sequencing batch membrane bioreactor and carries out biochemical treatment, strengthens the removal to the pollutent such as COD and ammonia nitrogen further, strengthening effluent quality.
A: the pre-treatment of distilled ammonia wastewater:
Embodiment 1
Distilled ammonia wastewater in equalizing tank slowly adds the vitriol oil under the state stirred, the pH controlling distilled ammonia wastewater is 2.6, then distilled ammonia wastewater is entered the top of rectangle Inner electrolysis reactor by infusion, carry out Inner electrolysis reaction, the filler of reactor is made up of iron and steel iron filings and activated carbon granule, and both are that the ratio of 1:1 is loaded in the reactor with volume ratio.Keep the residence time of distilled ammonia wastewater in Inner electrolysis reactor to be 0.5h, water outlet flows into Fenton oxidation pond.
Fenton oxidation pond is batch operation, and after the waste water in pond reaches 3/4, start stir and add the vitriol oil simultaneously, control ph is 2.8.Disposablely add ferrous sulfate solid, make the concentration of ferrous ion reach 100ppm, then slowly add the hydrogen peroxide solution that massfraction is 30%, make its concentration reach 900ppm.Under the state stirred, the controlled oxidization reaction times is 0.5h, and reacted waste water flows into coagulative precipitation tank.
Drip in coagulative precipitation tank massfraction be 10% NaOH solution regulate the pH of waste water to be 9.0, add the coagulant aids PAM of 1ppm, stir and staticly settle 25min after five minutes.After precipitation, the supernatant liquor of gained is pretreated distilled ammonia wastewater.
Test parameter in the embodiment 2 of pretreatment section and embodiment 3 is chosen with reference to table 1.
The operating parameters of each embodiment of table 1 pretreatment section
Main water-quality guideline in distilled ammonia wastewater is: COD:3500mg/L, ammonia nitrogen: 210mg/L, volatile phenol: 920mg/L, prussiate: 15mg/L, and each embodiment is after Inner electrolysis+Fenton oxidation+flocculation precipitation pretreatment, and the leading indicator of water outlet is as shown in table 2.
The each embodiment of table 2 pretreatment section is to the removal effect of pollutent
Through above-mentioned pretreated distilled ammonia wastewater, COD≤1500mg/L, ammonia nitrogen≤190mg/L, volatile phenol≤80mg/L, prussiate≤2mg/L, B/C >=0.3, the biodegradability of waste water is improve, for subsequent biochemical process creates good flow condition while effectively enhancing refractory organic matter destruction.
B: the biochemical treatment of distilled ammonia wastewater:
Embodiment 1:
Adopt sequencing batch membrane bioreactor technique (SBMBR), membrane bioreactor is built-inly put into bio-reactor by membrane module, and membrane module adopts PVDF hollow fiber microfiltration membrane.By adopting the mode of stirrings/aeration to control aerobic nitrification and anoxic denitrification environment, make whole system temporally the cycle experience in turn inflows, idle, react, discharge four operations.Seed sludge takes from the aerobic returned sluge in chemical plant, first puts it in reactor and tames, and stirs 2h in domestication by water inlet, and idle 5h, aerated reaction 15h, draining 2h, tame one month, sludge concentration is 9500mg/L.
Flow into operation: pretreated distilled ammonia wastewater enters the bottom of membrane bioreactor by infusion, the reaction tank flowing into membrane bioreactor is sprayed through water distributor, make the active sludge boiling be deposited in bottom reaction tank, by continuous stirring, mud is fully contacted with waste water, and now active sludge intermixture is in anoxic condition.It is 1.5h that control anoxic enters the waste water time, and wastewater pH controls 8.5.
Idle operation: the dead time of Controlling System is 4h, and the active sludge microorganism now in reactor continues the environment remaining anoxic, can make full use of into water high-enriched organics as denitrifying carbon source, what anti-nitration reaction was carried out is more fully thorough.
Reaction process: start gas blower and start to carry out aeration to sewage, while abundant disturbance film silk, decelerating membrane pollution, for the active sludge in membrane bioreactor provides sufficient oxygen, make it be in oxygen condition, it effectively can be degraded to the carbonaceous organic material in sewage.Simultaneously, ammonium oxidation in waste water is become nitrite nitrogen and nitrate nitrogen by nitrifier, and for anoxic phases provides sufficient electron acceptor(EA), aerated reaction time controling is at 15h, it is 7.5 that pH controls, aeration rate: flooding quantity (air water throughput ratio) controls at 25:1.Gas blower stops aeration, and reaction process terminates.
Discharge operation: under the negative pressure-pumping of suction pump or the effect of head difference, water and part small-molecule substance are through membrane module, become system water outlet through outlet pipeline, macromolecular substance, active sludge microorganism and inorganic particle are membrane module and are trapped in reactor.Drain time controls as 1.5h, and quantity discharged is 1/3 of reactor volume, after discharge operation terminates, closes suction pump, starts the circulation of next cycle.
System repeats inflow in turn, leaves unused, reacts, discharges four operations within the time subsequently, whole system is in anoxic, the aerobic state replaced all the time, intermittent water inflow and water outlet, and in reaction process latter stage via shore pipe and the remaining active sludge of mud valve periodic exhaustion.The mud production rate of SBMBR system is lower, and during test run, sludge quantity slightly increases, and does not occur sludge bulking, system run all right.
Test parameter in the embodiment 2 of biochemical section and embodiment 3 is chosen with reference to table 3.
The operating parameters of each embodiment of the biochemical section of table 3
After sequencing batch membrane bioreactor technique process, the leading indicator of each embodiment water outlet is as shown in table 4.
The each embodiment of the biochemical section of table 4 is to the removal effect of pollutent
From result in table 4, the distilled ammonia wastewater after above-mentioned biochemical treatment, COD≤100mg/L, ammonia nitrogen≤15mg/L, volatile phenol≤0.5mg/L, prussiate≤0.5mg/L, Process for Effluent water conditioning, can meet Wastewater Of Steel Industry first discharge standard.
Claims (3)
1. a treatment process for coking distilled ammonia wastewater, the method equipment used comprises equalizing tank, Inner electrolysis reactor, Fenton oxidation pond, coagulative precipitation tank and sequencing batch membrane bioreactor, it is characterized in that described method is undertaken by following operation:
A: the pre-treatment of distilled ammonia wastewater: first pre-treatment is carried out to distilled ammonia wastewater, the distilled ammonia wastewater collected is passed into equalizing tank, adds acid and its pH value is regulated, control the pH of waste water between 2.6 ~ 3.1, become acidic solution, to be satisfied with the requirement of Inner electrolysis reaction; Waste water enters Inner electrolysis reactor by infusion, and the residence time is 0.5-2.5h, and water outlet flows into Fenton oxidation pond;
Fenton oxidation pond is batch operation, under the state constantly stirred, adds acid, makes its pH value control between 2.8-3.2; Add ferrous sulfate solid subsequently, the concentration of ferrous ion is made to reach 100-300ppm, and then add the hydrogen peroxide solution that concentration is 900-1100ppm, under the state stirred, the controlled oxidization reaction times is 0.5-2h, and reacted waste water flows into coagulative precipitation tank;
Adding alkali lye in coagulative precipitation tank regulates the pH of waste water between 9-10, and add the coagulant aids PAM of 1ppm, stir and staticly settle 25-40min after five minutes, after precipitation, the supernatant liquor of gained is pretreated distilled ammonia wastewater;
B: the biochemical treatment of distilled ammonia wastewater: adopt sequencing batch membrane bioreactor technique, temporally the cycle is experienced inflows, idle, reaction in turn, discharges four operations;
Flow into operation: pretreated distilled ammonia wastewater enters the bottom of membrane bioreactor by infusion, the reaction tank flowing into membrane bioreactor is sprayed through water distributor, by continuous stirring, mud is fully contacted with distilled ammonia wastewater, it is 1.5-2.5h that control anoxic enters the distilled ammonia wastewater time, and distilled ammonia wastewater pH controls at 8.5-9.0;
Idle operation: period scope is 4-5h;
Reaction process: start gas blower and start to carry out aeration to sewage, the reaction times controls to control between 7.5-8.5 at 15-17h, pH, and aeration rate and flooding quantity control at 25-35:1;
Discharge operation: discharge activity time controls as 1.5-2.5h;
Repeat inflow subsequently in turn, leave unused, react, discharge four operations.
2. the treatment process of coking distilled ammonia wastewater according to claim 1, is characterized in that: the seed sludge concentration in described sequencing batch membrane bioreactor reaches 9500mg/L.
3. the treatment process of coking distilled ammonia wastewater according to claim 1, is characterized in that: in described discharge operation, distilled ammonia wastewater quantity discharged is partial discharge.
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| CN103880233B (en) * | 2014-02-26 | 2015-06-03 | 同济大学 | Residual heat recycling type coking wastewater deep treatment method |
| CN104944676B (en) * | 2014-03-28 | 2017-04-12 | 宝山钢铁股份有限公司 | Method for treating coking nanofiltration concentrated water |
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