CN205442947U - Coking wastewater treatment system - Google Patents
Coking wastewater treatment system Download PDFInfo
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- CN205442947U CN205442947U CN201521081062.6U CN201521081062U CN205442947U CN 205442947 U CN205442947 U CN 205442947U CN 201521081062 U CN201521081062 U CN 201521081062U CN 205442947 U CN205442947 U CN 205442947U
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Abstract
The utility model discloses a coking wastewater treatment system, including A2O biological denitrogenation dephosphorization system, AO reaction tank, coagulating sedimentation tank and the ozone oxidation reaction tower that couples in order. The utility model discloses not only get rid of efficiently, the oxidation rate is fast, goes out water stabilization of water quality moreover, no secondary pollution, and play water CODcr <= 80mgL after this technology is handled, ammonia nitrogen <= 10mgL, the phenol <= 0.3mgL that volatilizees, TP <= 1mgL, cyanide <= 0.2mgL goes out the standard that water CODcr and ammonia nitrogen etc. All can reach " make coke chemical industrial pollution thing emission standard " GB16171 -2012's table 2. This method implementation cost is lower, operation low cost, and the operational effect is stable, realizes the engineering scale easily, has wide application prospect in the aspect of coking wastewater treatment.
Description
Technical field
This utility model relates to a kind of Waste Water Treatment, is specially a kind of coking wastewater processing system.
Background technology
Being a kind of high CODcr, high phenol value, high ammonia nitrogen and the most intractable industrial organic waste water to coking chemical waste water, have colourity high, matter property is highly stable, and biodegradability is poor, ammonia nitrogen concentration high.At present, what domestic coke-oven plant was commonly used is the coking chemical waste water technological process with traditional biological denitrogenation processing as core, uses AO or with the A after AO process modification2/O、A/O2, bioremediation based on the biological reinforced technique such as O-A-O, be often aided with coagulating kinetics after biochemical treatment, the coking chemical waste water index after process is difficult to stably reach discharge standard, and particularly CODcr and total nitrogen the two index are difficult to reach emission request simultaneously.
Patent 201210408185.0 discloses the processing method of a kind of coking chemical waste water, including biochemical treatment and the advanced treatment process of coking chemical waste water of coking chemical waste water；Biochemical treatment uses A2O technique, advanced treating uses Inner electrolysis+Fenton oxidation+coagulating sedimentation+active carbon adsorption；High concentration coking is after this process, and effluent quality can reach the requirement of the integrated wastewater discharge standard of CODcr≤50mg/L, ammonia nitrogen≤8mg/L, volatile phenol≤0.3mg/L, total cyanogen≤0.2mg/L.Patent CN201010117965.0 discloses the advanced treatment process of a kind of coking chemical waste water, it is the coking chemical waste water the most successively after MBR Membrane Bioreactor for Wastewater Treatment, O3 contacted oxidation process, activated carbon adsorption process, reverse osmosis membrane processing of the coking chemical waste water after pretreatment and A/O biochemical treatment, production net circulating water can be met and supplement water water quality requirement.
Utility model content
The utility model discloses a kind of A2The coking wastewater processing system that O+AO+ catalytic ozonation method combines, for the thinking that the sustainable development offer of coal chemical enterprise is new.
In order to solve above-mentioned technical problem, this utility model provides following technical scheme:
A kind of coking wastewater processing system, including A2O biological carbon and phosphorous removal system, described A2The outfan of O biological carbon and phosphorous removal system is connected with the input in intermediate sedimentation pond, the outfan in described intermediate sedimentation pond is connected with the input of AO reaction tank, the described outfan of AO reaction tank is connected with the input of coagulative precipitation tank, and the outfan of described coagulative precipitation tank is connected with the input of ozone oxidation reaction tower.
Described A2O biological carbon and phosphorous removal system includes anaerobic reation pool, hypoxia response pond and the aerobic reaction tank being sequentially connected with.A2In the activated sludge of O biological carbon and phosphorous removal system, flora is mainly made up of nitrifier and denitrifying bacterium, polyP bacteria, and BOD5, SS in sewage and the nitrogen existed in a variety of manners and phosphorus are removed by microbiological deterioration.
At A2The aerobic section of O biological carbon and phosphorous removal system, maintains sludge concentration 3-4g/L, and hydraulic detention time is that 38-40h, DO by the ammonia nitrogen in sewage and the ammonia nitrogen of organic nitrogen ammonification one-tenth, by biological nitration effect, change into nitrate at 2-4mg/L, nitrobacteria；
At A2The anoxia section of O biological carbon and phosphorous removal system, sludge concentration 4-6g/L, hydraulic detention time is 12-15h, DO is at 0.2-0.5mg/L, the nitrate that internal reflux is brought into by denitrifying bacteria under stirring passes through biological denitrification, change into nitrogen to escape in air, thus reach the purpose of denitrogenation；
At A2The anaerobism section of O biological carbon and phosphorous removal system, sludge concentration 4-6g/L, hydraulic detention time be 8-10h, DO be 0, in anaerobic pond, polyP bacteria release phosphorus, and absorbs the degradable Organic substances such as lower fatty acid；And at aerobic section, polyP bacteria excess absorbs phosphorus, and by the discharge of excess sludge, phosphorus is removed；
Further, described AO reaction tank is provided with carbon source supplementing device.Because the CODcr entered in AO pond, the second level is the highest, remaining carbon source is not enough to support and completes denitrification denitrogenation reaction.Carbon source needed for extra supplementary denitrification, improves the nitric efficiency of second level AO system.Described A2O biological carbon and phosphorous removal system and AO reaction tank are provided with nitrification liquid inner loop pipeline.
Further, described ozone oxidation reaction tower selects rustless steel or carbon steel material, and liner is provided with resistance to oxidation corrosion-inhibiting coating；The water inlet of described ozone oxidation reaction tower is arranged on above tower body, and the entrance of ozone is arranged on described ozone oxidation reaction tower bottom, is provided with titanium plate micro-hole aerator at described ozone inlet；Former water water inlet above tower body flows into tower body, lower section is flowed out, ozone from reaction tower lower entrances through titanium plate micro-hole aerator air inlet, in tower, ozone concentration maintains 20-300mg/L, become counter current contacting mode with former water, in ozone oxidation reaction tower, be filled with the loaded catalyst that 20%-30% tower body is long-pending.Sewage ozone, catalyst synergy under, utilize the strong oxidizing property of ozone by inorganization for biochemical substances part difficult in waste water or be degraded to can biochemical substances, larger molecular organics is decomposed into small organic molecule, and the ozone not utilized in catalytic ozonation reaction tower need to carry out ozone decomposed by tail gas breaking plant.Water outlet after catalytic ozonation tower processes i.e. can reach the standard of the table 2 of " coking chemistry emission of industrial pollutants standard " GB16171-2012.
Further, described coagulative precipitation tank is provided with and described A2The sludge return pipe that O biological carbon and phosphorous removal system connects.
Further, described coagulative precipitation tank is provided with flocculant chemicals dosing plant.
The novel operation principle of this use is: initially enter A through the pretreated coking chemical waste water of dephenolize oil removing2O biological carbon and phosphorous removal system, the preliminary BOD removed in sewage5, SS and the nitrogen existed in a variety of manners and phosphorus, coking chemical waste water experiences the environment of anaerobic/anoxic/aerobic successively, and subsequently into AO reaction tank, coking chemical waste water experiences the environment of anoxia/aerobic successively, further completes denitrogenation in AO reaction tank；Through A2The CODcr of O Yu AO biochemical reaction stage waste water is down to about 150-250mg/l, remaining CODcr is mainly the heterocyclic compound of the difficult for biological degradation such as indole, quinoline, AO reaction tank water outlet enters ozone oxidation reaction tower after coagulative precipitation tank dosing precipitates, sewage ozone, catalyst synergy under, being cleaned further, the water outlet after catalytic ozonation tower processes i.e. can reach discharge standard.
Coking wastewater processing system of the present utility model, having combined A2O biological carbon and phosphorous removal system, AO reaction tank, coagulative precipitation tank and ozone oxidation reaction tower, not only removal efficiency is high, and oxidation rate is fast, and stable effluent quality, non-secondary pollution, the water outlet CODcr≤80mg/L after this PROCESS FOR TREATMENT, ammonia nitrogen≤10mg/L, volatile phenol≤0.3mg/L, TP≤1mg/L, cyanide≤0.2mg/L, water outlet CODcrThe standard of the table 2 of " coking chemistry emission of industrial pollutants standard " GB16171-2012 all can be reached with ammonia nitrogen etc..This method implementation cost is relatively low, and operating cost is cheap, and operational effect is stable, easily realizes project scale, has broad application prospects in terms of Treatment of Coking Effluent.
Accompanying drawing explanation
Accompanying drawing is used for providing being further appreciated by of the present utility model, and constitutes a part for description, is used for explaining this utility model, is not intended that restriction of the present utility model together with embodiment of the present utility model.In the accompanying drawings:
Fig. 1 is the block diagram of this utility model coking wastewater processing system.
Detailed description of the invention
Below in conjunction with accompanying drawing, preferred embodiment of the present utility model is illustrated, it will be appreciated that preferred embodiment described herein is merely to illustrate and explains this utility model, be not used to limit this utility model.
Embodiment 1
As it is shown in figure 1, a kind of coking wastewater processing system, including A2O biological carbon and phosphorous removal system, A2The outfan of O biological carbon and phosphorous removal system is connected with the input in intermediate sedimentation pond, the outfan in intermediate sedimentation pond is connected with the input of AO reaction tank, the outfan of AO reaction tank is connected with the input of coagulative precipitation tank, and the outfan of coagulative precipitation tank is connected with the input of ozone oxidation reaction tower.A2O biological carbon and phosphorous removal system and AO reaction tank are provided with nitrification liquid inner loop pipeline, A2The sludge return pipe that O biological carbon and phosphorous removal system connects.
A2O biological carbon and phosphorous removal system includes anaerobic reation pool, hypoxia response pond and the aerobic reaction tank being sequentially connected with.A2In the activated sludge of O biological carbon and phosphorous removal system, flora is mainly made up of nitrifier and denitrifying bacterium, polyP bacteria, and BOD5, SS in sewage and the nitrogen existed in a variety of manners and phosphorus are removed by microbiological deterioration.
At A2The aerobic section of O biological carbon and phosphorous removal system, maintains sludge concentration 3-4g/L, and hydraulic detention time is that 38-40h, DO by the ammonia nitrogen in sewage and the ammonia nitrogen of organic nitrogen ammonification one-tenth, by biological nitration effect, change into nitrate at 2-4mg/L, nitrobacteria；
At A2The anoxia section of O biological carbon and phosphorous removal system, sludge concentration 4-6g/L, hydraulic detention time is 12-15h, DO is at 0.2-0.5mg/L, the nitrate that internal reflux is brought into by denitrifying bacteria under stirring passes through biological denitrification, change into nitrogen to escape in air, thus reach the purpose of denitrogenation；
At A2The anaerobism section of O biological carbon and phosphorous removal system, sludge concentration 4-6g/L, hydraulic detention time be 8-10h, DO be 0, in anaerobic pond, polyP bacteria release phosphorus, and absorbs the degradable Organic substances such as lower fatty acid；And at aerobic section, polyP bacteria excess absorbs phosphorus, and by the discharge of excess sludge, phosphorus is removed；
It is provided with carbon source supplementing device on described AO reaction tank, supplements carbon source needed for denitrification, improve the nitric efficiency of second level AO system.
Stainless steel selected by ozone oxidation reaction tower, and liner is provided with resistance to oxidation corrosion-inhibiting coating；The water inlet of ozone oxidation reaction tower is arranged on above tower body, and the entrance of ozone is arranged on described ozone oxidation reaction tower bottom, is provided with titanium plate micro-hole aerator at described ozone inlet；Former water water inlet above tower body flows into tower body, lower section is flowed out, ozone from reaction tower lower entrances through titanium plate micro-hole aerator air inlet, in tower, ozone concentration maintains 20-300mg/L, become counter current contacting mode with former water, in ozone oxidation reaction tower, be filled with the loaded catalyst that 20%-30% tower body is long-pending.Sewage ozone, catalyst synergy under, utilize the strong oxidizing property of ozone by inorganization for biochemical substances part difficult in waste water or be degraded to can biochemical substances, larger molecular organics is decomposed into small organic molecule, and the ozone not utilized in catalytic ozonation reaction tower need to carry out ozone decomposed by tail gas breaking plant.
Flocculant chemicals dosing plant it is provided with on coagulative precipitation tank.
The novel operation principle of this use is: initially enter A through the pretreated coking chemical waste water of dephenolize oil removing2O biological carbon and phosphorous removal system, the preliminary BOD removed in sewage5, SS and the nitrogen existed in a variety of manners and phosphorus, coking chemical waste water experiences the environment of anaerobic/anoxic/aerobic successively, and subsequently into AO reaction tank, coking chemical waste water experiences the environment of anoxia/aerobic successively, further completes denitrogenation in AO reaction tank；Through A2The CODcr of O Yu AO biochemical reaction stage waste water is down to about 150-250mg/l, remaining CODcr is mainly the heterocyclic compound of the difficult for biological degradation such as indole, quinoline, AO reaction tank water outlet enters ozone oxidation reaction tower after coagulative precipitation tank dosing precipitates, sewage ozone, catalyst synergy under, being cleaned further, the water outlet after catalytic ozonation tower processes i.e. can reach discharge standard.
Coking wastewater processing system of the present utility model, A2O biological carbon and phosphorous removal system, AO reaction tank, coagulative precipitation tank and ozone oxidation reaction tower are combined, not only removal efficiency is high, and oxidation rate is fast, and stable effluent quality, non-secondary pollution, water outlet CODcr≤80mg/L after this PROCESS FOR TREATMENT, ammonia nitrogen≤10mg/L, volatile phenol≤0.3mg/L, TP≤1mg/L, cyanide≤0.2mg/L.
Last it is noted that the foregoing is only preferred embodiment of the present utility model, it is not limited to this utility model, although this utility model being described in detail with reference to previous embodiment, for a person skilled in the art, technical scheme described in foregoing embodiments still can be modified by it, or wherein portion of techniques feature is carried out equivalent.All within spirit of the present utility model and principle, any modification, equivalent substitution and improvement etc. made, within should be included in protection domain of the present utility model.
Claims (10)
1. a coking wastewater processing system, it is characterised in that include A2O biological carbon and phosphorous removal system, described A2The outfan of O biological carbon and phosphorous removal system is connected with the input of AO reaction tank, and the described outfan of AO reaction tank is connected with the input of coagulative precipitation tank, and the outfan of described coagulative precipitation tank is connected with the input of ozone oxidation reaction tower.
2. a kind of coking wastewater processing system as claimed in claim 1, it is characterised in that described A2O biological carbon and phosphorous removal system includes anaerobic reation pool, hypoxia response pond and the aerobic reaction tank being sequentially connected with.
3. a kind of coking wastewater processing system as claimed in claim 1, it is characterized in that, the water inlet of described ozone oxidation reaction tower is arranged on above tower body, and the entrance of ozone is arranged on described ozone oxidation reaction tower bottom, is provided with titanium plate micro-hole aerator at described ozone inlet.
4. a kind of coking wastewater processing system as described in any one of claim 1-3, it is characterised in that described A2O biological carbon and phosphorous removal system and AO reaction tank are provided with nitrification liquid inner loop pipeline.
5. a kind of coking wastewater processing system as described in any one of claim 1-3, it is characterised in that described coagulative precipitation tank is provided with and described A2The sludge return pipe that O biological carbon and phosphorous removal system connects.
6. a kind of coking wastewater processing system as claimed in claim 3, it is characterised in that be provided with resistance to oxidation corrosion-inhibiting coating in described ozone oxidation reaction tower.
7. a kind of coking wastewater processing system as described in claim 3 or 6, it is characterised in that be filled with the loaded catalyst that 20%-30% tower body is long-pending in described ozone oxidation reaction tower.
8. a kind of coking wastewater processing system as described in claim 3 or 6, it is characterised in that described ozone oxidation reaction tower is outside equipped with tail gas breaking plant.
9. a kind of coking wastewater processing system as claimed in claim 1, it is characterised in that be provided with carbon source supplementing device on described AO reaction tank.
10. a kind of coking wastewater processing system as claimed in claim 1, it is characterised in that be provided with flocculant chemicals dosing plant on described coagulative precipitation tank.
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| CN201521081062.6U CN205442947U (en) | 2015-12-21 | 2015-12-21 | Coking wastewater treatment system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108217947A (en) * | 2018-02-14 | 2018-06-29 | 温志军 | A kind of batch-type control method of sewage disposal AO and AAO techniques |
| CN111072217A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Method for advanced treatment and recycling of saliferous oil refining wastewater |
| CN113277681A (en) * | 2021-06-11 | 2021-08-20 | 湖北近水环境工程有限公司 | Ecological treatment method of wastewater |
| CN115215439A (en) * | 2022-08-19 | 2022-10-21 | 中建生态环境集团有限公司 | Sewage deep denitrification device based on two-stage AO double-reflux process and operation method |
-
2015
- 2015-12-21 CN CN201521081062.6U patent/CN205442947U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108217947A (en) * | 2018-02-14 | 2018-06-29 | 温志军 | A kind of batch-type control method of sewage disposal AO and AAO techniques |
| CN111072217A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Method for advanced treatment and recycling of saliferous oil refining wastewater |
| CN113277681A (en) * | 2021-06-11 | 2021-08-20 | 湖北近水环境工程有限公司 | Ecological treatment method of wastewater |
| CN115215439A (en) * | 2022-08-19 | 2022-10-21 | 中建生态环境集团有限公司 | Sewage deep denitrification device based on two-stage AO double-reflux process and operation method |
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