CN110759593A - Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow - Google Patents

Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow Download PDF

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CN110759593A
CN110759593A CN201911073873.4A CN201911073873A CN110759593A CN 110759593 A CN110759593 A CN 110759593A CN 201911073873 A CN201911073873 A CN 201911073873A CN 110759593 A CN110759593 A CN 110759593A
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tank
coking wastewater
controlled
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anoxic
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王凯
尹君贤
杨飞
董明
张成金
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Acre Coking and Refractory Engineering Consulting Corp MCC
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Acre Coking and Refractory Engineering Consulting Corp MCC
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step

Abstract

The invention relates to a process for treating coking wastewater by sectional water inlet and multistage A/O, pretreated coking wastewater firstly enters an anaerobic tank for hydrolysis acidification reaction, the effluent of the anaerobic tank is divided into 3 parts according to the proportion and respectively enters an anoxic tank of a three-stage A/O system; the coking wastewater is subjected to denitrification reaction in the anoxic tank of each grade of A/O system, and COD degradation and ammonia nitrogen nitration reaction are performed in the aerobic tank of each grade of A/O system; and the effluent of the aerobic tank of the last stage A/O system enters a secondary sedimentation tank, sludge flows back to the anoxic tank of the first stage A/O system after mud-water separation, and the supernatant of the secondary sedimentation tank enters a subsequent coking wastewater advanced treatment unit. On the premise of ensuring that the total nitrogen of the effluent reaches the standard, the method does not need to add an external carbon source and does not need to reflux the nitrifying liquid, and has stable treatment effect; thereby achieving the purposes of saving the operation cost and reducing the construction cost.

Description

Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow
Technical Field
The invention relates to the technical field of coking wastewater treatment, in particular to a process for treating coking wastewater by multistage A/O (anaerobic/oxic) through sectional water inflow.
Background
The coking wastewater mainly comes from coking, coal gas purification processes and chemical product refining processes, wherein ammonia distillation wastewater generated in the ammonia distillation process is taken as a main source, and the pollutant components are complex and have high concentration. Typical coking wastewater pollutant indexes are as follows: the COD concentration is 3000-5000 mg/L, the ammonia nitrogen concentration is 100-200 mg/L, the total nitrogen concentration is 250-350 mg/L, and the phenol concentration is 600-800 mg/L. In addition, nitrogen heterocyclic compounds, cyanides, and the like are also included.
At present, typical coking wastewater treatment technologies of domestic and foreign coking plants mainly adopt biological methods, including an A/0 (anoxic/aerobic) method, an A2/O (anaerobic/anoxic/aerobic) method, an A/O/O (anoxic/aerobic) method, an A2/O2 ((anaerobic/anoxic/aerobic) method and the like, and effluent indexes of coking wastewater subjected to biological treatment can basically reach COD (chemical oxygen demand) less than 300mg/L and NH (ammonia) less than 300mg/L3the-N is less than 25mg/L, and the effluent can be used for quenching coke and the like after further advanced treatment.
With the promulgation of the discharge standard of pollutants for coking chemical industry (GB16171-2012), strict requirements are put on the total nitrogen of the effluent from the coking wastewater treatment, wherein TN is less than 20mg/L when the effluent is directly discharged. In order to achieve the purpose of removing total nitrogen, the main process adopted by the coking wastewater at present is two-section A/O, the requirement of denitrification on a carbon source is met by adding glucose, sodium acetate and the like into a second-section A tank, and although the total nitrogen can reach the standard after the process is adopted, a large amount of carbon source needs to be added; meanwhile, a large amount of return nitrification liquid is needed to meet the requirement of denitrification; the coking wastewater treatment cost is increased, and the enterprise burden is increased.
Disclosure of Invention
The invention provides a process for treating coking wastewater by multistage A/O (anoxic/oxic) by sectional water inflow, which does not need to add an external carbon source or nitrifying liquid reflux on the premise of ensuring that the total nitrogen of effluent reaches the standard, and has stable treatment effect; thereby achieving the purposes of saving the operation cost and reducing the construction cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
a process for treating coking wastewater by sectional water inlet and multistage A/O comprises the steps of firstly, feeding pretreated coking wastewater into an anaerobic tank for hydrolysis acidification reaction, dividing the effluent of the anaerobic tank into 3 parts according to a proportion, and respectively feeding the 3 parts of effluent into an anoxic tank of a three-stage A/O system; the coking wastewater is subjected to denitrification reaction in the anoxic tank of each grade of A/O system, and COD degradation and ammonia nitrogen nitration reaction are performed in the aerobic tank of each grade of A/O system; and the effluent of the aerobic tank of the last stage A/O system enters a secondary sedimentation tank, sludge flows back to the anoxic tank of the first stage A/O system after mud-water separation, and the supernatant of the secondary sedimentation tank enters a subsequent coking wastewater advanced treatment unit.
The pretreatment process of the coking wastewater is used for removing heavy oil, emulsified oil and dissolved oil contained in the wastewater.
The anaerobic tank is internally provided with a fixed filler for fixing the growth of anaerobic microorganisms, and NaH is added into the anaerobic tank2PO4The adding amount is controlled according to the maintenance of the total phosphorus concentration in the anaerobic tank to be 0.5-1 mg/L, the hydraulic retention time of the coking wastewater in the anaerobic tank is 8-12 hours, and the temperature is 25-35 ℃.
When the effluent of the anaerobic tank enters an anoxic tank of the three-stage A/O system, the proportion of the coking wastewater quantity Q in the first-stage A/O system, the second-stage A/O system and the third-stage A/O system is as follows: 60-70%, 20-30% and 10-20%.
The anoxic tank volume of the first stage A/O system is (0.6-0.7) x Qx (30-50) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the volume of the aerobic tank of the first stage A/O system is (0.6-0.7) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The anoxic tank volume of the second stage A/O system is (0.2-0.3) x Q x (40-60) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the aerobic tank volume of the second stage A/O system is (0.2-0.3) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The anoxic pond volume of the third-stage A/O system is (0.1-0.2) x Q x (50-80) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; aerobic tank capacity of third-stage A/O systemThe product is (0.1 to 0.2) x Q x (150 to 200) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The surface load of the secondary sedimentation tank is 1-1.5 m3/m2h, the sludge reflux ratio is 100 to 200 percent.
And (3) maintaining the pH value of the aerobic tanks of the A/O systems at all levels by adding sodium carbonate or sodium hydroxide, wherein the adding amount is controlled according to the maintenance of the pH value of each aerobic tank to be 7.0-8.0.
Compared with the prior art, the invention has the beneficial effects that:
1) no additional carbon source is needed, and the operation cost is reduced; the carbon-nitrogen ratio of the coking wastewater is about 10: 1-20: 1, and the coking wastewater contains sufficient carbon source for denitrification utilization, and the carbon source in the coking wastewater is utilized to the maximum extent without additional carbon source, so that the wastewater running cost is reduced;
2) the return flow of the nitrifying liquid is not needed, so that the operating cost is saved; compared with the traditional process, the invention has no nitration liquid reflux system, thereby reducing the running power consumption and saving the running cost;
3) the construction cost is reduced; the process of the invention is not provided with a nitrifying liquid reflux system, and simultaneously only the last section of the aerobic tank is provided with a secondary sedimentation tank, so that the construction investment cost can be reduced.
Drawings
FIG. 1 is a process flow diagram of a sectional water inlet multistage A/O coking wastewater treatment process according to the invention.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in figure 1, the process for treating coking wastewater by sectional water inlet and multistage A/O comprises the steps of firstly enabling pretreated coking wastewater to enter an anaerobic tank for hydrolysis acidification reaction, dividing effluent of the anaerobic tank into 3 parts according to a proportion, and respectively entering an anoxic tank of a three-stage A/O system; the coking wastewater is subjected to denitrification reaction in the anoxic tank of each grade of A/O system, and COD degradation and ammonia nitrogen nitration reaction are performed in the aerobic tank of each grade of A/O system; and the effluent of the aerobic tank of the last stage A/O system enters a secondary sedimentation tank, sludge flows back to the anoxic tank of the first stage A/O system after mud-water separation, and the supernatant of the secondary sedimentation tank enters a subsequent coking wastewater advanced treatment unit.
The pretreatment process of the coking wastewater is used for removing heavy oil, emulsified oil and dissolved oil contained in the wastewater.
The anaerobic tank is internally provided with a fixed filler for fixing the growth of anaerobic microorganisms, and NaH is added into the anaerobic tank2PO4The adding amount is controlled according to the maintenance of the total phosphorus concentration in the anaerobic tank to be 0.5-1 mg/L, the hydraulic retention time of the coking wastewater in the anaerobic tank is 8-12 hours, and the temperature is 25-35 ℃.
When the effluent of the anaerobic tank enters an anoxic tank of the three-stage A/O system, the proportion of the coking wastewater quantity Q in the first-stage A/O system, the second-stage A/O system and the third-stage A/O system is as follows: 60-70%, 20-30% and 10-20%.
The anoxic tank volume of the first stage A/O system is (0.6-0.7) x Qx (30-50) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the volume of the aerobic tank of the first stage A/O system is (0.6-0.7) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The anoxic tank volume of the second stage A/O system is (0.2-0.3) x Q x (40-60) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the aerobic tank volume of the second stage A/O system is (0.2-0.3) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The anoxic pond volume of the third-stage A/O system is (0.1-0.2) x Q x (50-80) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the aerobic tank volume of the third stage A/O system is (0.1-0.2) x Q x (150-200) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The surface of the secondary sedimentation tank is negativeThe load is 1-1.5 m3/m2h, the sludge reflux ratio is 100 to 200 percent.
And (3) maintaining the pH value of the aerobic tanks of the A/O systems at all levels by adding sodium carbonate or sodium hydroxide, wherein the adding amount is controlled according to the maintenance of the pH value of each aerobic tank to be 7.0-8.0.
The following examples are carried out on the premise of the technical scheme of the invention, and detailed embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
As shown in fig. 1, in the following embodiment, the anoxic tank in the first stage a/O system is referred to as a first anoxic tank, the aerobic tank in the first stage a/O system is referred to as a first aerobic tank, the anoxic tank in the second stage a/O system is referred to as a second anoxic tank, the aerobic tank in the second stage a/O system is referred to as a second aerobic tank, the anoxic tank in the third stage a/O system is referred to as a third anoxic tank, and the aerobic tank in the third stage a/O system is referred to as a third aerobic tank.
[ example 1 ]
The treatment capacity of the coking wastewater of a certain coking plant is 40m3H, the water quality index of the pretreated coking wastewater is as follows: the Chemical Oxygen Demand (COD) is 2500-3000 mg/L, the cyanide is 20-30 mg/L, the volatile phenol is 400-500 mg/L, the sulfide is 20-30 mg/L, the petroleum is 20-50 mg/L, the ammonia nitrogen is 50-100 mg/L, and the pH value is 7.5-8.5.
The pretreated coking wastewater firstly enters an anaerobic tank, a fixed filler is arranged in the tank, and the refractory organic matters and the nitrogen-containing heterocyclic compounds in the coking wastewater undergo anaerobic hydrolysis acidification reaction to achieve the effect of converting open chains into micromolecular organic matters. The B/C of the waste water is improved, and the biodegradability is enhanced. NaH is added into the anaerobic tank2PO4The adding amount can maintain the total phosphorus concentration to be 0.5-1 mg/L; the coking wastewater stays in the anaerobic tank for 16 hours under the water temperature of 25-35 ℃; the dissolved oxygen is controlled below 0.2 mg/L.
The water yield of the anaerobic tank is about 60 percent, the water enters the first anoxic tank and is mixed with the sludge returned by the secondary sedimentation tank, and the denitrifying bacteria convert the nitrate into nitrogen by utilizing a carbon source in the coking wastewater;the first anoxic pond is provided with a submersible stirrer with the volume of 1200m3The water temperature is 20-35 ℃, the pH value is 7.0-7.5, and the dissolved oxygen is controlled below 0.5 mg/L.
The effluent of the first anoxic tank enters a first aerobic tank, a liftable microporous aerator is arranged in the tank, and toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the coking wastewater are biodegraded by adopting an activated sludge process, so that the ammonia nitrogen is subjected to nitration reaction; the first aerobic tank has a volume of 1920m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the first aerobic tank enters a second anoxic tank and is mixed with coking wastewater accounting for 30% of the effluent of the anaerobic tank, and the denitrifying bacteria convert nitrate into nitrogen by using a carbon source in the effluent of the anaerobic tank; the first anoxic tank is provided with a submersible stirrer with the volume of 600m3The water temperature is 20-35 ℃, the pH value is 7.0-7.5, and the dissolved oxygen is controlled below 0.5 mg/L.
The effluent of the second anoxic tank enters a second aerobic tank, a liftable microporous aerator is arranged in the second aerobic tank, and toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the coking wastewater are biodegraded and converted into CO by adopting an activated sludge process2And H2O, carrying out nitration reaction on ammonia nitrogen; the volume of the second aerobic tank is 960m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the second aerobic tank enters a third anoxic tank and is mixed with coking wastewater accounting for 10% of the effluent of the anaerobic tank, and the denitrifying bacteria convert nitrate into nitrogen by using a carbon source in the effluent of the anaerobic tank; the third anoxic pond is provided with a submersible stirrer with the volume of 320m3The dissolved oxygen is controlled to be less than 0.5 mg/L.
The effluent of the third anoxic tank enters a third aerobic tank, a liftable microporous aerator is arranged in the third aerobic tank, and toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the wastewater are biodegraded and converted into CO by adopting an activated sludge process2And H2O, ammonia nitrogen is subjected to nitration reaction and converted into nitric acidSalt nitrogen; the volume of the third aerobic tank is 800m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the third aerobic tank enters a secondary sedimentation tank for sludge-water separation, and the surface load of the secondary sedimentation tank is 1-1.5 m3/m2And h, refluxing the sludge precipitated to the bottom of the tank to the first anoxic tank, wherein the reflux ratio is controlled to be 100-200%.
In the embodiment, the total nitrogen of the effluent of the secondary sedimentation tank is 15-20 mg/L, and meets the requirements of direct discharge standards (total nitrogen is less than 20mg/L) in Table 2 of 'emission standards for pollutants in coking chemical industry' (GB 16171-2012).
[ example 2 ]
In this example, the coking wastewater of a certain coking plant was treated at a treatment capacity of 70m3H, the water quality index of the pretreated coking wastewater is as follows: 3000-3500 mg/L of COD, 30-40 mg/L of cyanide, 500-600 mg/L of volatile phenol, 30-50 mg/L of sulfide, 40-50 mg/L of petroleum, 100-120 mg/L of ammonia nitrogen and 7.5-8.5 of pH value.
The pretreated coking wastewater firstly enters an anaerobic tank, a fixed filler is arranged in the anaerobic tank, and the refractory organic matters and the nitrogen-containing heterocyclic compounds in the coking wastewater undergo anaerobic hydrolysis acidification reaction to achieve the effect of converting open chains into small molecular organic matters. The B/C of the coking wastewater is improved, and the biodegradability is enhanced. NaH is added into the anaerobic tank2PO4The adding amount can maintain the total phosphorus concentration to be 0.5-1 mg/L; the coking wastewater stays in the anaerobic tank for 12 hours under the water temperature of 25-35 ℃; the dissolved oxygen is controlled below 0.2 mg/L.
The water yield of the anaerobic tank is about 70 percent, the water enters the first anoxic tank and is mixed with the sludge returned by the secondary sedimentation tank, and the denitrifying bacteria convert the nitrate into nitrogen by utilizing the carbon source in the wastewater; the first anoxic tank is provided with a submersible stirrer with a volume of 1960m3The water temperature is 20-35 ℃, the pH value is 7.0-7.5, and the dissolved oxygen is controlled below 0.5 mg/L.
The effluent of the first anoxic tank enters a first aerobic tank, a liftable microporous aerator is arranged in the first aerobic tank, and phenol and cyanide in the wastewater are treated by an activated sludge processToxic and harmful substances such as sulfide, polycyclic aromatic hydrocarbon and the like are biologically reduced, and the ammonia nitrogen is subjected to nitration reaction; the volume of the first aerobic tank is 4900m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the first aerobic tank enters a second anoxic tank and is mixed with coking wastewater accounting for 20% of the effluent of the anaerobic tank, and the denitrifying bacteria convert nitrate into nitrogen by using a carbon source in the effluent of the anaerobic tank; a submersible stirrer with the volume of 700m is arranged in the first anoxic pond3The water temperature is 20-35 ℃, the pH value is 7.0-7.5, and the dissolved oxygen is controlled below 0.5 mg/L.
The effluent of the second anoxic tank enters a second aerobic tank, a liftable microporous aerator is arranged in the second aerobic tank, and toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the wastewater are biodegraded and converted into CO by adopting an activated sludge process2And H2O, carrying out nitration reaction on ammonia nitrogen; the volume of the second aerobic tank is 1400m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the second aerobic tank enters a third anoxic tank and is mixed with coking wastewater accounting for 10% of the effluent of the anaerobic tank, and the denitrifying bacteria convert nitrate into nitrogen by using a carbon source in the effluent of the anaerobic tank; the third anoxic pond is provided with a submersible stirrer with the volume of 560m3The dissolved oxygen is controlled to be less than 0.5 mg/L.
The effluent of the third anoxic tank enters a third aerobic tank, a liftable microporous aerator is arranged in the third aerobic tank, and toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the wastewater are biodegraded and converted into CO by adopting an activated sludge process2And H2O, carrying out nitration reaction on ammonia nitrogen and converting into nitrate nitrogen; the third aerobic pool has a volume of 1400m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
The effluent of the third aerobic tank enters a secondary sedimentation tank for sludge-water separation, and the surface load of the secondary sedimentation tank is 1-1.5 m3/m2And h, refluxing the sludge precipitated to the bottom of the tank to the first anoxic tank, wherein the reflux ratio is controlled to be 100-200%.
In the embodiment, the total nitrogen of the effluent of the secondary sedimentation tank is 13-19 mg/L, and meets the requirements of direct discharge standards (total nitrogen is less than 20mg/L) in Table 2 of 'emission standards for pollutants in coking chemical industry' (GB 16171-2012).
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.

Claims (9)

1. A process for treating coking wastewater by sectional water inlet and multistage A/O is characterized in that pretreated coking wastewater firstly enters an anaerobic tank for hydrolysis acidification reaction, and effluent of the anaerobic tank is divided into 3 parts according to a proportion and respectively enters an anoxic tank of a three-stage A/O system; the coking wastewater is subjected to denitrification reaction in the anoxic tank of each grade of A/O system, and COD degradation and ammonia nitrogen nitration reaction are performed in the aerobic tank of each grade of A/O system; and the effluent of the aerobic tank of the last stage A/O system enters a secondary sedimentation tank, sludge flows back to the anoxic tank of the first stage A/O system after mud-water separation, and the supernatant of the secondary sedimentation tank enters a subsequent coking wastewater advanced treatment unit.
2. The process for multistage A/O treatment of coking wastewater with staged water inlet according to claim 1, wherein the pretreatment of coking wastewater is used to remove heavy oil, emulsified oil and dissolved oil contained in the wastewater.
3. The process for multistage A/O treatment of coking wastewater with staged influent as claimed in claim 1, wherein the anaerobic tank is filled with a fixed filler for fixing the growth of anaerobic microorganisms, and NaH is added into the anaerobic tank2PO4The adding amount is controlled according to the maintenance of the total phosphorus concentration in the anaerobic tank to be 0.5-1 mg/L, and the hydraulic retention time of the coking wastewater in the anaerobic tank is 8-12h, the temperature is 25-35 ℃.
4. The process for treating coking wastewater by multistage A/O with staged water inlet according to claim 1, wherein when the effluent of the anaerobic tank enters the anoxic tank of the three-stage A/O system, the distribution ratio of the coking wastewater quantity Q in the first stage A/O system, the second stage A/O system and the third stage A/O system is as follows: 60-70%, 20-30% and 10-20%.
5. The process of multistage A/O coking wastewater treatment with staged water inflow according to claim 1, wherein the anoxic tank volume of the first stage A/O system is (0.6-0.7) XQX (30-50) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the volume of the aerobic tank of the first stage A/O system is (0.6-0.7) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
6. The process of multistage A/O coking wastewater treatment with staged water inflow according to claim 1, wherein the anoxic tank volume of the second stage A/O system is (0.2-0.3) xQx (40-60) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the aerobic tank volume of the second stage A/O system is (0.2-0.3) x Q x (80-100) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
7. The process for multistage A/O coking wastewater treatment by staged water inflow according to claim 1, wherein the anoxic tank volume of the third stage A/O system is (0.1-0.2) xQx (50-80) m3A submersible stirrer is arranged in the anoxic tank, and dissolved oxygen is controlled to be below 0.5 mg/L; the aerobic tank volume of the third stage A/O system is (0.1-0.2) x Q x (150-200) m3The dissolved oxygen is controlled to be 4-5 mg/L, the pH value is controlled to be 7.0-8.0, the temperature is controlled to be 20-30 ℃, and the sludge concentration is 3-4 g/L.
8. The process for multistage A/O coking wastewater treatment by using sectional inflow according to claim 1, wherein the surface load of the secondary sedimentation tank is 1-1.5 m3/m2h, the sludge reflux ratio is 100 to 200 percent.
9. The process for multistage A/O treatment of coking wastewater through sectional water inflow according to claim 1, wherein the pH value of the aerobic tanks of each stage of the A/O system is maintained by adding sodium carbonate or sodium hydroxide, and the adding amount is controlled according to the maintenance of the pH value of each aerobic tank to be 7.0-8.0.
CN201911073873.4A 2019-11-06 2019-11-06 Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow Pending CN110759593A (en)

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CN111233151A (en) * 2020-03-17 2020-06-05 山东太平洋环保股份有限公司 Efficient synchronous nitrogen and phosphorus removal system and method for high-nitrogen and phosphorus wastewater
CN112374696A (en) * 2020-11-09 2021-02-19 河北先河正合环境科技有限公司 System and method for treating sewage by multistage multi-point water inflow enhanced denitrification
CN112679049A (en) * 2020-12-30 2021-04-20 中冶焦耐(大连)工程技术有限公司 Method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR
CN113024026A (en) * 2021-03-10 2021-06-25 河北协同水处理技术有限公司 High-efficiency biological denitrification process for coking wastewater
CN117263390A (en) * 2023-11-21 2023-12-22 深圳永清水务有限责任公司 Biochemical treatment method for high-COD (chemical oxygen demand) high-ammonia-nitrogen wastewater
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