CN101602564A - A kind of treatment process of coking chemical waste water - Google Patents
A kind of treatment process of coking chemical waste water Download PDFInfo
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- CN101602564A CN101602564A CNA2009101812922A CN200910181292A CN101602564A CN 101602564 A CN101602564 A CN 101602564A CN A2009101812922 A CNA2009101812922 A CN A2009101812922A CN 200910181292 A CN200910181292 A CN 200910181292A CN 101602564 A CN101602564 A CN 101602564A
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
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- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 2
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- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
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- 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 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
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- ZMZDMBWJUHKJPS-UHFFFAOYSA-M Thiocyanate anion Chemical compound [S-]C#N ZMZDMBWJUHKJPS-UHFFFAOYSA-M 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a kind of treatment process of coking chemical waste water, belong to field of waste water treatment.Step is: Coking Plant Wastewater enters equalizing tank and carries out after water quality and quantity regulates, enter hydrolytic tank successively, anoxic pond, preaeration tank, preliminary sedimentation tank, Aerobic Pond, second pond and coagulation reaction tank are handled, wherein hydrolytic tank and preaeration tank inner filling biological rope filler, preliminary sedimentation tank mud passes back into hydrolytic tank and anoxic pond respectively, the second pond clear liquor passes back into anoxic pond, and Aerobic Pond adopts MBBR.The biological rope filler biofilm time of adopting among the present invention is short, and the biomass height does not need back flushing, strong shock resistance; MBBR can be fixed a large amount of generation times of long nitrifier, and does not have blocking problem.The present invention can remove the ammonia nitrogen and the organism of coking chemical waste water middle and high concentration, and water outlet COD after treatment and ammonia nitrogen can reach national sewage comprehensive emission standard (GB9878-1996) primary standard simultaneously.
Description
Technical field
The present invention relates to the treatment process of coking chemical waste water, belong to technical field of waste water processing, a kind of method that adopts active sludge and microbial film combined system Treatment of Wastewater in Coking of more specifically saying so.
Background technology
Coking chemical waste water is the trade effluent that produces in coal high temperature carbonization, gas purification, product recovery and tar, crude benzene refining process etc.Coking chemical waste water is except inorganic pollution beyond the region of objective existences such as the ammonia nitrogen that contains high density, prussiate, thiocyanide, sulfide, also contains organic pollutants such as the heterogeneous ring compound of phenolic compound, polycyclic aromatic hydrocarbons (PAHs) and nitrogenous, oxygen, sulphur etc. and fatty compounds.Ammonia nitrogen has toxicity to hydrobiont, and is one of " arch-criminal " of causing body eutrophication; Phenolic compound belongs to prototype matter poisonous substance, to all toxic effect of all biologies; PAHs and heterogeneous ring compound not only are difficult to biological degradation, common still " three cause " material.If coking chemical waste water is not handled and a large amount of discharging thus, not only can cause the severe contamination of environment, also can directly threaten human beings'health simultaneously.
At present, the treatment process of coking chemical waste water mainly contains physico-chemical process, biochemical process and materialization-biochemistry method for combined use.Physico-chemical process mainly contains absorption, coagulating sedimentation, little electrolysis, electrolysis, catalyzed oxidation etc.Higher by physico-chemical process Treatment of Wastewater in Coking cost merely, it is mainly used in PRETREATMENT OF THE COKING CHEMICAL WASTER WATER or advanced treatment at present.Processing cost is low because of having for biochemical process, the characteristics of non-secondary pollution etc. become the main method of current Treatment of Coking Effluent.Wherein conventional activated sludge process can effectively be removed phenol and the cyanogen class material in the waste water, but its adaptability to the variation of the influent quality water yield is lower, and is very poor to hardly degraded organic substance and ammonia nitrogen treatment effect, is difficult to reach emission standard.In order to remove ammonia nitrogen and organism simultaneously, in recent years, biological denitrification process causes people's attention gradually and becomes the main method of Treatment of Coking Effluent gradually, generally adopts anaerobic-aerobic (A/O) or anaerobic-anoxic-aerobic (A
1-A
2-O) activated sludge process.These technologies are owing to utilized the different degradation characteristics of anaerobism, double oxygen bacterium and aerobic bacteria, compare with conventional activated sludge process, significantly improvement is being arranged aspect removal COD and the ammonia nitrogen, but since coking chemical waste water to contain difficult degradation toxic organic compound kind many, the characteristics that water quality and quantity is complicated and changeable make A/O isoreactivity mud technology easily be hit, and particularly aerobic section autotrophy nitrifier is long owing to generation time, be hit the back recovery slowly, and nitrification efficiency descends.When nitrification liquid is back in the anoxic reacter, because it is not thorough that nitration reaction is carried out, nitric nitrogen and nitrite nitrogen content are less, the carbon source of denitrification consumption will correspondingly reduce, cause anoxic reacter COD clearance to descend, the organism of difficult degradation is fully degraded not, anoxic reacter water outlet COD raises, flow into the growth that aerobic reactor has promoted heterotrophic bacterium again, nitrifier is suppressed, rate of nitrification descends, and such circulation makes technology water outlet COD such as A/O and ammonia nitrogen be difficult to simultaneously up to standard.
Chinese patent application CN 2647845Y discloses and has adopted anaerobic fluidized bed, the anoxic fluidized-bed method as bio-reactor, has improved the treatment effect to the coking chemical waste water ammonia nitrogen in high density.Chinese patent application CN1686863A discloses the technology of biomembrance process anaerobic hydrolysis/anoxic/catalytic oxidation/biological aerated filter Treatment of Wastewater in Coking, the anaerobic pond filler is haydite, gac, coke or zeolite particulate filler in this technology, rubble or slag block filler, plastics Ball-type packing, semi soft packing or elastic solid filler; The anoxic pond filler is haydite, gac, coke, quartz sand, hard coal or zeolite particulate filler, plastics Ball-type packing, semi soft packing or elastic solid filler; Contact-oxidation pool is mainly used in de-carbon, the main nitration reaction that takes place in the BAF, and biophase forms nitrifier advantage section along the packed height layering at certain altitude, improves nitrification effect.Chinese patent application CN 101113065A discloses a kind of method that adopts bio-carrier-active sludge compounding technology anaerobic/anoxic/aerobic decarburization/aerobic nitrification Treatment of Wastewater in Coking, all establish in the biochemical reactor and hang or suspension folding and expanding formula Ball-type packing, add microorganism active excitation agent in the anoxic section, improve the active sludge proterties, improve biofilm biomass.Chinese patent application CN 101215068A discloses a kind of coking chemical waste water biological filter facture, anaerobic/anoxic/Aerobic Pond is in series by the filter tank respectively, filtrate is spherical ceramic grain filter or irregular shape ceramic grain filter, adopt regular back flushing to remove the mud and the suspended substance of accumulation in the filter tank, and drive the microbubble in anaerobism and the anoxic pond.These technologies have improved the biochemical treatment effect of coking chemical waste water to a certain extent, but biological fluidized bed exists complex structure, three phase separation difficulty, the high shortcoming of power consumption; The microbubble that anaerobism and anoxic filter tank produce can be detained in the filter tank for a long time, occupy the filter tank effective reaction space for a long time, reduce processing efficiency, also there is the blocking problem that easily hardens in some biofilm packings in addition, need frequent back flushing, cause the treatment effect instability.
Summary of the invention
1. invent the technical problem that will solve
Problem at the existing biological treatment existence of coking chemical waste water, the invention provides a kind of treatment process of coking chemical waste water, can be so that the biomass height, anti-impact force is strong, and water outlet COD after treatment and ammonia nitrogen can reach national sewage comprehensive emission standard (GB9878-1996) primary standard simultaneously.
2. technical scheme of the present invention is as follows:
A kind of treatment process of coking chemical waste water the steps include:
(1) Coking Plant Wastewater enters that equalizing tank is laggard goes into hydrolytic tank, and hydrolytic tank adopts active sludge and microbial film composite algorithm, upflowing water distribution;
(2) water outlet of hydrolytic tank enters anoxic pond, and anoxic pond adopts activated sludge process, is provided with perforated pipe at the bottom of the pond as water distributor, mechanical stirring;
(3) the anoxic pond water outlet enters preaeration tank, and preaeration tank adopts active sludge and microbial film composite algorithm equally, and aerating apparatus is arranged at the bottom of the pond;
(4) the preaeration tank water outlet is through the preliminary sedimentation tank post precipitation, and supernatant liquor enters Aerobic Pond, and thickened sludge passes back into hydrolytic tank and anoxic pond;
(5) Aerobic Pond adopts MBBR, adds alkali lye at water-in, at the bottom of its pond aerating apparatus is set;
(6) the Aerobic Pond water outlet enters the second pond precipitation, and top clear liquor partial reflux is gone into anoxic pond, and part enters coagulation basin;
(7) add flocculation agent and coagulant aids in coagulation reactor, mixed solution flows into coagulative precipitation tank to carry out discharging after the precipitation process.
Equalizing tank is mainly regulated the water quality and quantity and the water temperature of waste water, reduces the impact to hydrolytic tank.Waste water enters equalizing tank, carries out aeration and dilution adjusting, control dissolved oxygen concentration＜0.5mg/L.
Hydrolytic tank adopts the upflowing water distribution, mainly is by the acidication effect, and some difficult for biological degradation macromolecular substance in the waste water are carried out open loop, chain rupture, makes it be easy to biological degradation, improves the biodegradability of waste water.Hang biological rope in the reactor, the wire rope core periphery is the ring-type fine-fibered, diameter 35～50mm, and material is polypropylene, vinylon, nylon or their two kinds and multiple combination.This filler has excellent adsorptive power, and mud had both adhered to also easily to be peeled off easily, and product structure has not susceptible to plugging characteristic, can keep a large amount of microorganisms.
Anoxic reacter adopts activated sludge process, is that carbon source is carried out anti-nitration reaction with organism in the effusive waste water of hydrolytic tank, and intensified anti-nitrated performance adopts mechanical stirring to make the nitrogen of generation discharge system timely.
The main organism of further removing in the waste water of preaeration tank hangs biological rope in the pond, perforated pipe aerating regulation is adopted in the bottom, and dissolved oxygen concentration is 1～2mg/L.After the preaeration tank water outlet entered the preliminary sedimentation tank clarification, thickened sludge passed back into hydrolytic tank and anoxic pond, and control of reflux ratio is 0.2～0.8: 1.
Aerobic Pond is a MBBR, and nitration reaction mainly takes place.Fill Kaldnes type filler in the reactor, the high 9mm of filler, diameter are 10～25mm, and density is 0.95～0.98g/cm
3, material is polypropylene or polyethylene, and its shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, filler filling ratio volume ratio is 30～60%.Add the consumption of alkali lye at the reactor inlet place, be about under the neutral condition, add 0.6～0.7g yellow soda ash with every gram ammonia nitrogen in the solution and calculate the amount that adds, make pH remain on 7～8 in water inlet with additional nitration reaction pair basicity.
Micro-hole aerator is equipped with in the aerobic moving bed biofilm reactor bottom, and filler relies on aeration to pump in reactor, and mass transfer effect is better, and oxygen transfer efficiency is higher, and biomembranous activity is higher on the filler.Owing to the shearing force of water and the frictional force that carrier movement is produced, the filling surface microbial film can come off by nature, so can not cause obstruction, need not back flushing in addition, also need not mud and refluxes.The reactor water outlet is provided with small-bore mesh screen, and after the mixed solution that MBBR comes out entered the second pond clarification, a part passed back into anoxic pond, and reflux ratio is 3～7: 1, and another part enters coagulation basin.
Add flocculation agent in the depositing technology and carry out flocculation sediment, flocculation sediment technology mainly comprises: flocculant concentration facility, flocculation tank and final deposition pool.Flocculation agent adopts molysite or aluminium salt, and coagulant aids adopts polyacrylamide.Depositing technology does not have specific limited to flocculation agent, can select other flocculation agents yet.
3. beneficial effect of the present invention is:
(1) provides a kind of treatment process of coking chemical waste water,, can remove fast according to the characteristics of coking chemical waste water ammonia nitrogen concentration height and organism difficult degradation.
(2) the inner filled biomass rope of hydrolytic tank and preaeration tank filler makes that the biofilm time short, the biomass height, do not need back flushing, anti-impact force is strong, and Aerobic Pond adopts MBBR, can fix a large amount of generation times of long nitrifier, and not have blocking problem.
(3) when not adding the materialization processing, the water outlet ammonia nitrogen reaches (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ", and COD reaches secondary discharge standard; When adopting materialization to handle, water outlet COD and ammonia nitrogen all reach first discharge standard.
(4) occupation area of equipment required for the present invention is little, and used filler biofilm is fast, does not need back flushing, manages simple and conveniently, and running cost is low, treatment effect is stable.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Embodiment
Embodiment 1
As Fig. 1, in certain Coking Plant Wastewater treating processes, water inlet COD is 800～1300mg/L, and ammonia nitrogen is 60～100mg/L, and pH is 7.5～8.5.Waste water is gone into hydrolytic tank through equalizing tank regulating pondage and water quality are laggard, and sludge concentration is 5500～7000mg/L in the hydrolytic tank, inner filling biological rope filler, the wire rope core periphery is the ring-type fine-fibered, and material is nylon and polypropylene, diameter 35mm, adopt the upflowing water distribution, hydraulic detention time is 10h.The hydrolytic tank water outlet enters anoxic pond from the bottom, establishes mechanical stirring device in the anoxic pond, and sludge concentration is 4000～5000mg/L, and hydraulic detention time is 13h.Flow into preaeration tank through the anoxic pond processed waste water, filling biological rope filler in the preaeration tank, material is a polypropylene, diameter 100mm, pond bottom hole pipe aeration, dissolved oxygen (DO) concentration is 1～2mg/L, hydraulic detention time is 5h.Enter the preliminary sedimentation tank precipitation through the preaeration tank processed waste water, the bottom thickened sludge passes back into hydrolytic tank and anoxic pond, and reflux ratio was respectively 0.2: 1 and 0.4: 1, and the top clear liquor enters aerobic moving bed biofilm reactor (MBBR).The aerobic moving bed biofilm reactor water-in adds alkali lye, adds 0.6 yellow soda ash with every gram ammonia nitrogen and calculates the amount that adds; Add Kaldnes type filler in the pond, diameter 15mm, the material polypropylene, the filler shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, the filler stopping composition is 30% (volume ratio), and dissolved oxygen (DO) concentration is 4～6mg/L, and hydraulic detention time is 34h.Water outlet enters second pond, and after precipitate and separate, a top clear liquor part passes back into anoxic pond, reflux ratio is 3: 1, and rest part enters coagulation-settlement process, and flocculation agent adopts polymerize aluminum chloride, coagulant aids adopts polyacrylamide, and dosage is respectively 400mg/L and 3mg/L.
After above-mentioned art breading, final outflow water COD and ammonia nitrogen satisfy (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ".
Embodiment 2
As Fig. 1, in certain Coking Plant Wastewater treating processes, water inlet COD is 1000～2000mg/L, and ammonia nitrogen is 80～220mg/L, and pH is 7.0～8.5.Waste water is gone into hydrolytic tank through equalizing tank regulating pondage and water quality are laggard, and sludge concentration is 6000～7500mg/L in the hydrolytic tank, inner filling biological rope filler, the wire rope core periphery is the ring-type fine-fibered, and material is a polypropylene, diameter 35mm, adopt the upflowing water distribution, hydraulic detention time is 12h.The hydrolytic tank water outlet enters anoxic pond from the bottom, establishes mechanical stirring device in the anoxic pond, and sludge concentration is 4000～5500mg/L, and hydraulic detention time is 16h.Flow into preaeration tank through the anoxic pond processed waste water, filling biological rope filler in the preaeration tank, material is a polypropylene, diameter 45mm, pond bottom hole pipe aeration, dissolved oxygen (DO) concentration is 1～2mg/L, hydraulic detention time is 6h.Enter the preliminary sedimentation tank precipitation through the preaeration tank processed waste water, the bottom thickened sludge passes back into hydrolytic tank and anoxic pond, and reflux ratio was respectively 0.8: 1 and 0.2: 1, and the top clear liquor enters aerobic moving bed biofilm reactor (MBBR).The aerobic moving bed biofilm reactor water-in adds alkali lye, adds 0.7g yellow soda ash with every gram ammonia nitrogen in the solution and calculates dosage; Add Kaldnes type filler in the pond, material is a polypropylene, diameter 10mm, the filler shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, the filler stopping composition is 45% (volume ratio), and dissolved oxygen (DO) concentration is 4～6mg/L, and hydraulic detention time is 40h.Water outlet enters second pond, and after precipitate and separate, a top clear liquor part passes back into anoxic pond, reflux ratio is 5: 1, and rest part enters coagulation-settlement process, and flocculation agent adopts ferric sulfate, coagulant aids adopts polyacrylamide, and dosage is respectively 550mg/L and 3mg/L.
After above-mentioned art breading, final outflow water COD and ammonia nitrogen satisfy (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ".
Embodiment 3
As Fig. 1, in certain Coking Plant Wastewater treating processes, water inlet COD is 1500～2500mg/L, and ammonia nitrogen is 70～210mg/L, and pH is 7.5～9.0.Waste water is gone into hydrolytic tank through equalizing tank regulating pondage and water quality are laggard, sludge concentration is 6000～8000mg/L in the hydrolytic tank, inner filling biological rope filler, the wire rope core periphery is the ring-type fine-fibered, material is nylon, vinylon and polypropylene, diameter 50mm adopts the upflowing water distribution, and hydraulic detention time is 13h.The hydrolytic tank water outlet enters anoxic pond from the bottom, establishes mechanical stirring device in the anoxic pond, and sludge concentration is 5000～6000mg/L, and hydraulic detention time is 17.5h.Flow into preaeration tank through the anoxic pond processed waste water, filling biological rope filler in the preaeration tank, material is a polypropylene, diameter 45mm, pond bottom hole pipe aeration, dissolved oxygen (DO) concentration is 1～2mg/L, hydraulic detention time is 7h.Enter the preliminary sedimentation tank precipitation through the preaeration tank processed waste water, the bottom thickened sludge passes back into hydrolytic tank and anoxic pond, and reflux ratio was respectively 0.2: 1 and 0.8: 1, and the top clear liquor enters aerobic moving bed biofilm reactor (MBBR).The aerobic moving bed biofilm reactor water-in adds alkali lye, every gram ammonia nitrogen adds 0.66g yellow soda ash, adds Kaldnes type filler in the pond, and material is a polyethylene, diameter 25mm, the filler shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, the filler stopping composition is 50% (volume ratio), and dissolved oxygen concentration (DO) is 4～6mg/L, and hydraulic detention time is 42.5h.Water outlet enters second pond, and after precipitate and separate, a top clear liquor part passes back into anoxic pond, reflux ratio is 6: 1, and rest part enters coagulation-settlement process, and flocculation agent adopts ferric sulfate, coagulant aids adopts polyacrylamide, and dosage is respectively 750mg/L and 4mg/L.
After above-mentioned art breading, final outflow water COD and ammonia nitrogen satisfy (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ".
Embodiment 4
As Fig. 1, in certain Coking Plant Wastewater treating processes, water inlet COD is 1000～1700mg/L, and ammonia nitrogen is 90～160mg/L, and pH is 8.0～9.5.Waste water is gone into hydrolytic tank through equalizing tank regulating pondage and water quality are laggard, and sludge concentration is 6000～7500mg/L in the hydrolytic tank, inner filling biological rope filler, the wire rope core periphery is the ring-type fine-fibered, and material is a polypropylene, diameter 100mm, adopt the upflowing water distribution, hydraulic detention time is 10.5h.The hydrolytic tank water outlet enters anoxic pond from the bottom, establishes mechanical stirring device in the anoxic pond, and sludge concentration is 4000～5000mg/L, and hydraulic detention time is 14.5h.Flow into preaeration tank through the anoxic pond processed waste water, filling biological rope filler in the preaeration tank, material is a polypropylene, diameter 35mm, pond bottom hole pipe aeration, dissolved oxygen (DO) concentration is 1～2mg/L, hydraulic detention time is 5.5h.Enter the preliminary sedimentation tank precipitation through the preaeration tank processed waste water, the bottom thickened sludge passes back into hydrolytic tank and anoxic pond, and reflux ratio was respectively 0.2: 1 and 0.3: 1, and the top clear liquor enters aerobic moving bed biofilm reactor (MBBR).The aerobic moving bed biofilm reactor water-in adds alkali lye, every gram ammonia nitrogen adds 0.63g yellow soda ash, adds Kaldnes type filler in the pond, and material is a polyethylene, diameter 10mm, the filler shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, the filler stopping composition is 40% (volume ratio), and dissolved oxygen concentration (DO) is 4～6mg/L, and hydraulic detention time is 36h.Water outlet enters second pond, and after precipitate and separate, a top clear liquor part passes back into anoxic pond, reflux ratio is 4: 1, and rest part enters coagulation-settlement process, and flocculation agent adopts polymerize aluminum chloride, coagulant aids adopts polyacrylamide, and dosage is respectively 500mg/L and 3mg/L.
After above-mentioned art breading, final outflow water COD and ammonia nitrogen satisfy (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ".
Embodiment 5
As Fig. 1, in certain Coking Plant Wastewater treating processes, water inlet COD is 1000～3000mg/L, and ammonia nitrogen is 110～280mg/L, and pH is 7.0～9.0.Waste water is gone into hydrolytic tank through equalizing tank regulating pondage and water quality are laggard, and sludge concentration is 7000～8000mg/L in the hydrolytic tank, inner filling biological rope filler, the wire rope core periphery is the ring-type fine-fibered, and material is a polypropylene, diameter 50mm, adopt the upflowing water distribution, hydraulic detention time is 15h.The hydrolytic tank water outlet enters anoxic pond from the bottom, establishes mechanical stirring device in the anoxic pond, and sludge concentration is 5000～6000mg/L, and hydraulic detention time is 20h.Flow into preaeration tank through the anoxic pond processed waste water, filling biological rope filler in the preaeration tank, material is a polypropylene, diameter 45mm, pond bottom hole pipe aeration, dissolved oxygen (DO) concentration is 1～2mg/L, hydraulic detention time is 8h.Enter the preliminary sedimentation tank precipitation through the preaeration tank processed waste water, the bottom thickened sludge passes back into hydrolytic tank and anoxic pond, and reflux ratio was respectively 0.3: 1 and 0.6: 1, and the top clear liquor enters aerobic moving bed biofilm reactor (MBBR).The aerobic moving bed biofilm reactor water-in adds alkali lye, every gram ammonia nitrogen adds 0.7g yellow soda ash, adds Kaldnes type filler in the pond, and material is a polypropylene, diameter 25mm, the filler shape is hollow cylinder, and column body has cross bracing, the outer wall belt vertical bar shape fin wing of post, the likeness in form gear, the filler stopping composition is 60% (volume ratio), and dissolved oxygen concentration (DO) is 4～6mg/L, and hydraulic detention time is 46h.Water outlet enters second pond, and after precipitate and separate, a top clear liquor part passes back into anoxic pond, reflux ratio is 7: 1, and rest part enters coagulation-settlement process, and flocculation agent adopts polymerize aluminum chloride, coagulant aids adopts polyacrylamide, and dosage is respectively 900mg/L and 4mg/L.
After above-mentioned art breading, final outflow water COD and ammonia nitrogen satisfy (GB8978-96) first discharge standard of country's " integrated wastewater discharge standard ".
Claims (8)
1, a kind of treatment process of coking chemical waste water is characterized in that concrete steps are:
(1) Coking Plant Wastewater enters that equalizing tank is laggard goes into hydrolytic tank, and hydrolytic tank adopts active sludge and microbial film composite algorithm, upflowing water distribution;
(2) water outlet of hydrolytic tank enters anoxic pond, and anoxic pond adopts activated sludge process, is provided with perforated pipe at the bottom of the pond as water distributor, mechanical stirring;
(3) the anoxic pond water outlet enters preaeration tank, and preaeration tank adopts active sludge and microbial film composite algorithm, and aerating apparatus is arranged at the bottom of the pond;
(4) the preaeration tank water outlet is through the preliminary sedimentation tank post precipitation, and supernatant liquor enters Aerobic Pond, and thickened sludge passes back into hydrolytic tank and anoxic pond;
(5) Aerobic Pond adopts MBBR, adds alkali lye at water-in, at the bottom of its pond aerating apparatus is set;
(6) the Aerobic Pond water outlet enters the second pond precipitation, and top clear liquor partial reflux is gone into anoxic pond, and part enters coagulation basin;
(7) add flocculation agent and coagulant aids in coagulation reactor, mixed solution flows into coagulative precipitation tank to carry out discharging after the precipitation process.
2, the treatment process of a kind of coking chemical waste water according to claim 1, it is characterized in that the inner filled biomass rope of preaeration tank filler in described step (1) hydrolytic tank and the step (3), diameter is 35～100mm, the wire rope core periphery is the ring-type fine-fibered, and material is polypropylene, vinylon, nylon or their two kinds and multiple combination.
3, the treatment process of a kind of coking chemical waste water according to claim 2 is characterized in that the preliminary sedimentation tank mud in the described step (3) passes back into hydrolytic tank and anoxic pond, and reflux ratio is 0.2～0.8: 1.
4, according to the treatment process of each described a kind of coking chemical waste water in the claim 1～3, it is characterized in that Aerobic Pond adopts MBBR in the described step (5), the filler of throwing is a Kaldnes type filler, density is 0.95～0.98g/cm
3, the high 9mm of filler, diameter are 10～25mm, and material is polypropylene or polyethylene, and filler filling ratio volume ratio is 30～60%.
5, according to the treatment process of each described a kind of coking chemical waste water in the claim 1～3, it is characterized in that the Aerobic Pond in the described step (5), adding alkali lye in ingress is sodium carbonate solution, adds 0.6～0.7g yellow soda ash with every gram ammonia nitrogen in the solution and calculates the amount that adds.
6, according to the treatment process of each described a kind of coking chemical waste water in the claim 1～3, it is characterized in that aerating apparatus is a micro-hole aerator in the described step (5), water outlet is provided with small-bore mesh screen.
7, according to the treatment process of each described a kind of coking chemical waste water in the claim 1～3, it is characterized in that the precipitation of two described in the described step (6) clear liquor passes back into anoxic pond, reflux ratio is 3～7: 1.
8, according to the treatment process of each described a kind of coking chemical waste water in the claim 1～3, it is characterized in that the coagulation reaction tank described in the step (7), the flocculation agent that adds is molysite or aluminium salt, coagulant aids is a polyacrylamide, and is provided with whipping appts.
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