CN104016548B - A kind of Biochemical Process for Treating Coke Plant Wastewater - Google Patents
A kind of Biochemical Process for Treating Coke Plant Wastewater Download PDFInfo
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Abstract
The present invention relates to a kind of Biochemical Process for Treating Coke Plant Wastewater, it comprises the steps: (1), and first coking chemical waste water enter in anaerobic biofilter carries out anaerobic hydrolysis reaction and Inner electrolysis reaction, in anaerobic biofilter, be wherein furnished with the Inner electrolysis filler that Inner electrolysis reaction occurs; (2) coking chemical waste water through anaerobic biofilter process enters A-O Biochemistry Reaction System, carries out anaerobic-aerobic biochemical treatment.The object of the invention is to the effect improving coking chemical waste water biochemical treatment, reduce dilution water consumption.
Description
Technical field
The present invention relates to a kind of Biochemical Process for Treating Coke Plant Wastewater, namely adopt the AAO biochemical treatment system of the filler-reinforced anaerobic biofilter of Inner electrolysis.
Background technology
Iron And Steel Industry is one of maximum industry of resource, energy consumption, needs to consume a large amount of coke, can produce seriously polluted reluctant coking chemical waste water in coke-oven plant's coking, gas purification and change product purification process in smelting process.Be still one of comparatively cost-effective method generally adopted at present by biochemical process Treatment of Wastewater in Coking, Treatment of Coking Effluent comprises the process of biological dephenolize cyanogen and biological denitrificaion process two kinds.In coking chemical waste water biological treatment, relate to aerobic, anaerobism, anoxic and autotrophy, heterotrophism and the foster numerous biotic populations be interweaved of holding concurrently.There is obvious capacity volume variance between contained pollutent in coking chemical waste water, is cause different biotic population in Treatment of Coking Effluent to have major cause unique separately.Although Treatment of Coking Effluent can adopt some municipal effluent biological treatment flow process sometimes, its design variable and operation control condition are different, and some municipal sewage treatment flow process is inapplicable in Treatment of Coking Effluent at all.
Because microorganism is difficult to tolerate organism, ammonia nitrogen and bio-toxicity material too high in coking chemical waste water, Treatment of Coking Effluent all can add the froth breaking water of about one times etc. as dilution water, causes coking chemical waste water amount greatly to increase.After full-fledged Treatment of Coking Effluent, the COD of water generally can be reduced to 150-300mg/L, but is difficult to the requirement reaching national grade one discharge standard, therefore generally all increases advanced oxidation process after precipitation again to reduce the COD of waste water in biochemical treatment; Ammonia nitrogen can reach or close to national grade one discharge standard 5mg/L, but there have many treatment plants to run to be not good yet, and water outlet ammonia nitrogen is far above Effluent criteria.
Summary of the invention
For existing Biochemical Process for Treating Coke Plant Wastewater, the invention provides the technique of a kind of reinforced anaerobic biological treatment.The object of the invention is to overcome existing technique not enough, solving coking chemical waste water biochemical treatment needs to add dilution water, produces shipwreck with problem up to standard.
The technical solution used in the present invention is as follows: a kind of Biochemical Process for Treating Coke Plant Wastewater, it comprises the steps:
(1) first coking chemical waste water enters in anaerobic biofilter (1) and carries out anaerobic hydrolysis reaction and Inner electrolysis reaction, in anaerobic biofilter, be wherein furnished with the Inner electrolysis filler (3) that Inner electrolysis reaction occurs;
(2) coking chemical waste water processed through anaerobic biofilter (1) enters A-O Biochemistry Reaction System, carries out anaerobic-aerobic biochemical treatment.
Wherein, A-O Biochemistry Reaction System comprises: anoxic pond (6), Aerobic Pond (7) and settling tank (8), there is anti-nitration reaction in the anoxic pond (6) that the coking chemical waste water wherein processed through anaerobic biofilter (1) first enters A-O Biochemistry Reaction System, there is nitration reaction, decyanization reaction and dephenolize reaction in the Aerobic Pond (7) that the coking chemical waste water after anoxic pond (6) process enters A-O Biochemistry Reaction System, the coking chemical waste water after Aerobic Pond (7) process enters settling tank (8) and precipitates.
Wherein, coking chemical waste water is 1-8 hour in anaerobic biofilter (1) residence time, is 10-120 minute with filler (3) duration of contact; Coking chemical waste water is 4-16 hour in anoxic pond (6) residence time of A-O Biochemistry Reaction System, and Aerobic Pond (7) residence time is 24-36 hour.Wherein coking chemical waste water is 29-60 hour in the residence time that anaerobic biofilter, anoxic pond and Aerobic Pond are total.
Wherein, coking chemical waste water is 4 hours in anaerobic biofilter (1) residence time, is 0.5 hour with filler (3) duration of contact; Coking chemical waste water is 12 hours in anoxic pond (6) residence time of A-O Biochemistry Reaction System, Aerobic Pond (7) residence time is 32 hours, and coking chemical waste water is 48 hours in the residence time that anaerobic biofilter, anoxic pond (6) and Aerobic Pond (7) are total.
Wherein, in A-O Biochemistry Reaction System, the sludge reflux of settling tank (8) is in Aerobic Pond (7) or anoxic pond (6), and backflow per-cent is 10%-200%.
Wherein, in A-O Biochemistry Reaction System, the nitrification liquid of settling tank (8) is back in Aerobic Pond (7) or anoxic pond (6), and backflow per-cent is 50%-600%.Sludge reflux per-cent is 50%.Nitrification liquid backflow per-cent is 300%.
Wherein, Inner electrolysis filler (3) adopts high temperature sintering to make, and the particle diameter of filler is 0.5-40cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:3 to 3:1.Wherein, the temperature of high temperature sintering is 500-1000 DEG C.
Wherein, described filler (3) is placed in container (2), and described container (2) is can stacking form, and there is perforation container (2) both sides.
Wherein, there is lifting upper arm (4) described container (2) both sides; Spud pile (5) is provided with, for fixed container (2) at the bottom of the pond of anaerobic biofilter (1).
Wherein, be the organism of more easily degrading by the Decomposition of the anaerobion in anaerobic biofilter by the organic matter degradation in waste water.
Wherein, Inner electrolysis filler (3) is porous high surface area filler, makes the anaerobion in anaerobic biofilter adhere on it, forms anaerobe film; When coking chemical waste water flows through the filler hanging with described anaerobe film, the organism in waste water is degraded to the organism of more easily degrading by the anaerobion in microbial film.
Wherein, there is potential difference between iron-carbon granule and define multiple galvanic cell; Galvanic cell is with the low iron of current potential for negative electrode, and the carbon that current potential is high is anode, and Inner electrolysis reaction occurs in coking chemical waste water.
Wherein, Inner electrolysis reaction is specially: iron is corroded the iron ion becoming divalence and enters in coking chemical waste water solution; Hydroxide radical effect in iron ion and coking chemical waste water solution defines the ferrous hydroxide with coagulation, and there is a natural attraction between the sexes for particulate electronegative in itself and coking chemical waste water, forms throw out and remove; The macromole of difficult degradation in described solution adsorb by carbon granule and/or through iron ion above-mentioned flocculation reaction and reduce.
Present treatment technique is compared with conventional biochemical Treatment of Wastewater in Coking method, tool has the following advantages: (1) improves BOD/COD value when coking chemical waste water enters anoxic pond, useless Organic substance in water is more easily degraded by microorganisms, thus reduces the COD value of producing water.(2) reduce the COD value into water, in the COD value of coking chemical waste water is reduced to load that microorganism can bear, thus reduce or eliminate the interpolation of froth breaking water, decrease Treatment of Coking Effluent aquifer yield.(3) relative to traditional AAO biochemical treatment, anaerobic pond is changed into anaerobic biofilter; Relative to traditional AO biochemical treatment, using an equalizing tank transformation part as anaerobic biofilter.There is higher microorganism concn, better anaerobic digestion effect.(4) can transform in existing AAO technique or AO technique easily, cost of reducing investment outlay.
Accompanying drawing explanation
Fig. 1 is Inner electrolysis strengthening AAO biochemical treatment coking chemical waste water schematic diagram;
Embodiment
As shown in Figure 1, implement the equipment of Biochemical Process for Treating Coke Plant Wastewater, comprise anaerobic biofilter 1, A-O Biochemistry Reaction System; Wherein anaerobic biofilter 1 is communicated with A-O Biochemistry Reaction System; A-O Biochemistry Reaction System comprises: anoxic pond 6, Aerobic Pond 7 and settling tank 8, the front end of anoxic pond 6 is communicated with anaerobic biofilter 1, rear end is communicated with Aerobic Pond 7, Aerobic Pond 7 is communicated with settling tank 8, wherein, there is anti-nitration reaction in anoxic pond 6, nitration reaction, decyanization reaction and dephenolize reaction occur Aerobic Pond 7.Be furnished with filler 3 and containment system 2 thereof that Inner electrolysis reaction can occur in anaerobic biofilter 1, wherein the addition of filler 3 requires according to the size in pond, effluent quality and the factor such as wastewater flow is determined to add.Inner electrolysis filler 3 adopts sintering to make, and the temperature of high temperature sintering is 500-1000 DEG C.The particle diameter of filler is 0.5-40cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:3 to 3:1.State filler 3 and be placed in container 2, and described container 2 is can stacking form, and container 2 both sides there is perforation.There is lifting upper arm 4 described container 2 both sides; Spud pile 5 is provided with, for fixed container 2 at the bottom of the pond of anaerobic biofilter 1.
As shown in Figure 1, nitrification liquid backflow 9 is for be back to anaerobic pond 6 from settling tank 8, and sludge reflux 10 is for be back to Aerobic Pond 7 from settling tank 8.But the one shown in the more than Fig. 1 of backflow array mode.Can certainly be other reflux type: the sludge reflux of settling tank 8 is in anoxic pond 6.The nitrification liquid of settling tank 8 is back in Aerobic Pond 7.
Biochemical Process for Treating Coke Plant Wastewater principle is as follows: as shown in Figure 1, coking chemical waste water enters in anaerobic biofilter 1 and carries out anaerobic hydrolysis reaction and Inner electrolysis reaction, after reducing COD, raising B/C ratio, waste water enters A-O Biochemistry Reaction System, carries out conventional anaerobic-aerobic treatment.Coking chemical waste water enters anaerobic biofilter 1, carries out anaerobic acidification, is the short chain organism of more readily biodegradable, improves the bio-degradable of waste water by the Decomposition of the anaerobion in filter tank 1 by organic matter degradation.Inner electrolysis filler 3 in water is porous high surface area filler, and microorganism is adhered on it in a large number, and anaerobion part apposition growth, on filler 3, forms anaerobe film, part suspension growth between filtrate space.When effluent stream is through hanging with biomembranous filler 3, the organism in water is diffused into biofilm surface, and is converted into small molecules easily biodegradable organics by the microbiological deterioration in microbial film.Meanwhile, there is potential difference between iron-carbon granule and define numerous trickle galvanic cell.These trickle batteries become negative electrode with the iron that current potential is low, and the carbon that current potential is high does anode, and in containing the aqueous solution of acidic electrolyte bath, electrochemical reaction (Inner electrolysis reaction) occurs, iron is corroded the iron ion becoming divalence and enters solution.Iron ion and hydroxide radical effect define the ferrous hydroxide with coagulation, and there is a natural attraction between the sexes for the particulate with faint negative charge in it and pollutent, forms more stable throw out (being also iron mud) and remove.The macromole of some difficult degradations adsorb by carbon granule and/or through iron ion flocculation and reduce, thus BOD/COD is raised.Then coking chemical waste water enters follow-up anaerobic-aerobic biochemical treatment, and anti-nitration reaction occurs anoxic pond 6, and nitration reaction, decyanization reaction and dephenolize reaction occur Aerobic Pond 7.
Wherein, Inner electrolysis filler drops in the anaerobic biological pond of AAO biochemical treatment, or drop in the equalizing tank of AO biochemical treatment, transform the form of anaerobic biofilter 1 as, Inner electrolysis filler 3 is as the attachment filler of anaerobic biofilter 1, and filler is held by multiple cuboid container 2, and container has 2 sides to be cavernous, have handle can sling for crane, end face is that cover plate can be buckled extremely.The multiple containers being full of filler are closely deposited on anaerobic biofilter 1 one transverse section, and porose side is exposed towards both sides.During operation, intaking is entered by side, pond, by arriving water outlet side after packing layer.
In order to further describe invention, the embodiment of employing is as follows.Wherein embodiment is carried out according to aforesaid reaction principle.
Embodiment 1
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 500 DEG C, and the particle diameter of filler is 0.5cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:3.Wherein coking chemical waste water is 2 hours in anaerobic biofilter 1 residence time, is 20 minutes with filler 3 duration of contact; Coking chemical waste water is 6 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 26 hours.Wherein coking chemical waste water is 34 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in Aerobic Pond 7, and backflow per-cent is that in the nitrification liquid backflow anoxic pond 6 of settling tank 8 in 40%, A-O Biochemistry Reaction System, backflow per-cent is 100%.
Before reaction, the water quality of coking chemical waste water is: temperature 32 DEG C, pH10.45, COD3571mg/L, volatile phenol 533mg/L, total cyanide 57.8mg/L, ammonia nitrogen 65.6mg/L, total phosphorus 8.38mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 28 DEG C, pH7.10, COD141mg/L, volatile phenol 0.01mg/L, total cyanide 0.1mg/L, ammonia nitrogen 1.85mg/L, total phosphorus 0.09mg/L.Meet relevant emission standard.
Embodiment 2
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 800 DEG C, and the particle diameter of filler is 20cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 2:3.Wherein coking chemical waste water is 4 hours in anaerobic biofilter 1 residence time, is 30 minutes with filler 3 duration of contact; Coking chemical waste water is 12 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 32 hours.Wherein coking chemical waste water is 48 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in anoxic pond 6, and backflow per-cent is 100%.The nitrification liquid of settling tank 8 is back in Aerobic Pond 7, and backflow per-cent is 300%.
Before reaction, the water quality of coking chemical waste water is: temperature 33 DEG C, pH10.85, COD3600mg/L, volatile phenol 538mg/L, total cyanide 58.8mg/L, ammonia nitrogen 67.6mg/L, total phosphorus 8.78mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 27 DEG C, pH7.20, COD151mg/L, volatile phenol 0.015mg/L, total cyanide 0.12mg/L, ammonia nitrogen 1.86mg/L, total phosphorus 0.093mg/L.Meet relevant emission standard.
Embodiment 3
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 1000 DEG C, and the particle diameter of filler is 30cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 2:1.Wherein coking chemical waste water is 6 hours in anaerobic biofilter 1 residence time, is 80 minutes with filler 3 duration of contact; Coking chemical waste water is 14 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 30 hours.Wherein coking chemical waste water is 50 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in Aerobic Pond 7, and backflow per-cent is that the nitrification liquid of settling tank 8 in 150%, A-O Biochemistry Reaction System is back in Aerobic Pond 7, and backflow per-cent is 400%.
Before reaction, the water quality of coking chemical waste water is: temperature 35 DEG C, pH10.65, COD3511mg/L, volatile phenol 553mg/L, total cyanide 60.8mg/L, ammonia nitrogen 67.6mg/L, total phosphorus 8.88mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 29 DEG C, pH7.18, COD146mg/L, volatile phenol 0.017mg/L, total cyanide 0.14mg/L, ammonia nitrogen 1.89mg/L, total phosphorus 0.097mg/L.Meet relevant emission standard.
Embodiment 4
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 600 DEG C, and the particle diameter of filler is 8cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:1.Wherein coking chemical waste water is 8 hours in anaerobic biofilter 1 residence time, is 100 minutes with filler 3 duration of contact; Coking chemical waste water is 15 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 34 hours.Wherein coking chemical waste water is 57 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in anoxic pond 6, and backflow per-cent is 180%.The nitrification liquid of settling tank 8 is back in anoxic pond 6, and backflow per-cent is 500%.
Before reaction, the water quality of coking chemical waste water is: temperature 33 DEG C, pH11.51, COD3625mg/L, volatile phenol 540mg/L, total cyanide 58.1mg/L, ammonia nitrogen 65.1mg/L, total phosphorus 8.45mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 26 DEG C, pH7.14, COD143mg/L, volatile phenol 0.016mg/L, total cyanide 0.15mg/L, ammonia nitrogen 1.85mg/L, total phosphorus 0.091mg/L.Meet relevant emission standard.
Embodiment 5
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 1000 DEG C, and the particle diameter of filler is 40cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 3:1.Wherein coking chemical waste water is 8 hours in anaerobic biofilter 1 residence time, is 120 minutes with filler 3 duration of contact; Coking chemical waste water is 16 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 36 hours.Wherein coking chemical waste water is 60 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in anoxic pond 6, and backflow per-cent is 200%.The nitrification liquid of settling tank 8 is back in Aerobic Pond 7, and backflow per-cent is 600%.
Before reaction, the water quality of coking chemical waste water is: temperature 33 DEG C, pH11.56, COD3650mg/L, volatile phenol 545mg/L, total cyanide 59.7mg/L, ammonia nitrogen 64.1mg/L, total phosphorus 8.85mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 27 DEG C, pH7.01, COD130mg/L, volatile phenol 0.092mg/L, total cyanide 0.08mg/L, ammonia nitrogen 1.71mg/L, total phosphorus 0.08mg/L.Meet relevant emission standard.
Embodiment 6
Inner electrolysis filler 3 adopts high temperature sintering to make, and wherein sintering temperature is 500 DEG C, and the particle diameter of filler is 0.5cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:3.Wherein coking chemical waste water is 1 hour in anaerobic biofilter 1 residence time, is 10 minutes with filler 3 duration of contact; Coking chemical waste water is 4 hours in anoxic pond 6 residence time of A-O Biochemistry Reaction System, and Aerobic Pond 7 residence time is 24 hours.Wherein coking chemical waste water is 29 hours in the residence time that anaerobic biofilter 1, anoxic 6 pond and Aerobic Pond 7 are total.In A-O Biochemistry Reaction System, the sludge reflux of settling tank 8 is in Aerobic Pond 7, and backflow per-cent is the nitrification liquid backflow Aerobic Pond 7 of settling tank 8 in 20%, A-O Biochemistry Reaction System, and backflow per-cent is 50%.
Before reaction, the water quality of coking chemical waste water is: temperature 35 DEG C, pH9.10, COD3148mg/L, volatile phenol 403mg/L, total cyanide 45.8mg/L, ammonia nitrogen 50.6mg/L, total phosphorus 6.58mg/L.
After reaction, the water quality of coking chemical waste water water outlet is: temperature 29 DEG C, pH7.16, COD160mg/L, volatile phenol 0.019mg/L, total cyanide 0.18mg/L, ammonia nitrogen 1.98mg/L, total phosphorus 0.1mg/L.Meet relevant emission standard.
Claims (12)
1. a Biochemical Process for Treating Coke Plant Wastewater, it comprises the steps:
(1) first coking chemical waste water enters in anaerobic biofilter (1) and carries out anaerobic hydrolysis reaction and Inner electrolysis reaction, in anaerobic biofilter, be wherein furnished with the Inner electrolysis filler (3) that Inner electrolysis reaction occurs;
(2) coking chemical waste water processed through anaerobic biofilter (1) enters A-O Biochemistry Reaction System, carries out anaerobic-aerobic biochemical treatment;
Inner electrolysis filler (3) adopts high temperature sintering to make, and the particle diameter of Inner electrolysis filler is 0.5-40cm, and firing raw material is iron powder and carbon dust, and firing proportioning by the mass ratio of iron powder and carbon dust is 1:3 to 3:1; The temperature of high temperature sintering is 500-1000 DEG C.
2. treatment process according to claim 1, it is characterized in that, wherein, A-O Biochemistry Reaction System comprises: anoxic pond (6), Aerobic Pond (7) and settling tank (8), there is anti-nitration reaction in the anoxic pond (6) that the coking chemical waste water wherein processed through anaerobic biofilter (1) first enters A-O Biochemistry Reaction System, there is nitration reaction in the Aerobic Pond (7) that the coking chemical waste water after anoxic pond (6) process enters A-O Biochemistry Reaction System, decyanization reaction and dephenolize reaction, coking chemical waste water after Aerobic Pond (7) process enters settling tank (8) and precipitates.
3. treatment process according to claim 1 and 2, is characterized in that, wherein coking chemical waste water is 1-8 hour in anaerobic biofilter (1) residence time, is 10-120 minute with Inner electrolysis filler (3) duration of contact; Coking chemical waste water is 4-16 hour in anoxic pond (6) residence time of A-O Biochemistry Reaction System, and Aerobic Pond (7) residence time is 24-36 hour.
4. treatment process according to claim 3, is characterized in that, wherein coking chemical waste water is 29-60 hour in the residence time that anaerobic biofilter, anoxic pond and Aerobic Pond are total.
5. treatment process according to claim 4, is characterized in that, coking chemical waste water is 4 hours in anaerobic biofilter (1) residence time, is 0.5 hour with Inner electrolysis filler (3) duration of contact; Coking chemical waste water is 12 hours in anoxic pond (6) residence time of A-O Biochemistry Reaction System, Aerobic Pond (7) residence time is 32 hours, and coking chemical waste water is 48 hours in the residence time that anaerobic biofilter, anoxic pond (6) and Aerobic Pond (7) are total.
6. treatment process according to claim 2, is characterized in that, in A-O Biochemistry Reaction System, the sludge reflux of settling tank (8) is in Aerobic Pond (7) or anoxic pond (6), and backflow per-cent is 10%-200%.
7. treatment process according to claim 6, is characterized in that, sludge reflux per-cent is 50%.
8. treatment process according to claim 2, is characterized in that, in A-O Biochemistry Reaction System, the nitrification liquid of settling tank (8) is back in Aerobic Pond (7) or anoxic pond (6), and backflow per-cent is 50%-600%.
9. treatment process according to claim 8, is characterized in that, nitrification liquid backflow per-cent is 300%.
10. treatment process according to claim 1 and 2, it is characterized in that, described Inner electrolysis filler (3) is placed in container (2), and described container (2) is can stacking form, and there is perforation container (2) both sides, there is lifting upper arm (4) described container (2) both sides; Spud pile (5) is provided with, for fixing container (2) at the bottom of the pond of anaerobic biofilter (1).
11. treatment process according to claim 1 and 2, it is characterized in that, be the organism of more easily degrading by the Decomposition of the anaerobion in anaerobic biofilter by the organic matter degradation in waste water, Inner electrolysis filler (3) is porous high surface area filler, make the anaerobion in anaerobic biofilter adhere on it, form anaerobe film; When coking chemical waste water flows through the filler hanging with described anaerobe film, the organism in waste water is degraded to the organism of more easily degrading by the anaerobion in microbial film.
12. treatment process according to claim 1 and 2, is characterized in that, there is potential difference and define multiple galvanic cell between iron-carbon granule; Galvanic cell is with the low iron of current potential for negative electrode, and the carbon that current potential is high is anode, and Inner electrolysis reaction occurs in coking chemical waste water; Inner electrolysis reaction is specially: iron is corroded the iron ion becoming divalence and enters in coking chemical waste water solution; Hydroxide radical effect in iron ion and coking chemical waste water solution defines the ferrous hydroxide with coagulation, and there is a natural attraction between the sexes for particulate electronegative in itself and coking chemical waste water, forms throw out and remove; The macromole of difficult degradation in described solution adsorb by carbon granule and/or through iron ion flocculation reaction and reduce.
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| CN101456644A (en) * | 2007-12-11 | 2009-06-17 | 中国京冶工程技术有限公司 | Method for processing organic industrial effluent by catalytic reduction bio-ferric technique |
| WO2014012201A1 (en) * | 2012-07-14 | 2014-01-23 | Ling Liang | Method for removing total nitrogen during treatment of coking wastewater by using microorganisms |
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| CN101456644A (en) * | 2007-12-11 | 2009-06-17 | 中国京冶工程技术有限公司 | Method for processing organic industrial effluent by catalytic reduction bio-ferric technique |
| WO2014012201A1 (en) * | 2012-07-14 | 2014-01-23 | Ling Liang | Method for removing total nitrogen during treatment of coking wastewater by using microorganisms |
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| A-A-O法生物脱氮工艺在焦化废水处理中的应用;亓学山等;《山东化工》;20050430;第34卷(第2期);参见第34-35页第1节，第3.1节，图1 * |
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