CN113603302A - Coking wastewater reduction treatment method - Google Patents
Coking wastewater reduction treatment method Download PDFInfo
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- CN113603302A CN113603302A CN202110942791.XA CN202110942791A CN113603302A CN 113603302 A CN113603302 A CN 113603302A CN 202110942791 A CN202110942791 A CN 202110942791A CN 113603302 A CN113603302 A CN 113603302A
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- water
- tank
- effluent
- wastewater
- coking wastewater
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F5/12—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing nitrogen
- C02F5/125—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing nitrogen combined with inorganic substances
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Abstract
The invention relates to the technical field of industrial wastewater treatment, in particular to a coking wastewater reduction treatment method. After the coking wastewater is treated by the processes of regulating reservoir, air floatation degreasing, coagulating sedimentation, biochemical homogenizing pool, biological filter pool, secondary sedimentation pool, UV advanced ozone oxidation, ultrafiltration, reverse osmosis, chemical softening pool, sand filtration, resin, regulating reservoir, ultrafiltration, nanofiltration and bipolar membrane electrodialysis, the generated acid and alkali can be used for process recycling such as pH regulation in the treatment process, so that the resource utilization of the coking wastewater is realized, the outsourcing cost of reagents is reduced, the energy consumption in the process is low, the cost is low, the equipment is simple, the operation is easy, the treatment effect is stable, and the water treatment agent selected in the treatment process strengthens the treatment effect.
Description
Technical Field
The invention relates to the technical field of industrial wastewater treatment, in particular to a coking wastewater reduction treatment method.
Background
The coking wastewater is high-concentration organic wastewater which is toxic, harmful and difficult to degrade, wherein the organic matters comprise more phenol compounds and account for about half of the total organic matters, the organic matters also comprise polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and carbon and the like, and the inorganic pollutants mainly comprise ammonia nitrogen, cyanide, sulfide and thiocyanide.
At present, most of domestic wastewater treatment systems of coke-oven plants adopt primary treatment and secondary treatment processes, but in recent years, tertiary treatment processes are also adopted. The first-stage treatment refers to the recycling of pollutants in high-concentration wastewater, and comprises ammonia dephenolization, ammonia distillation, final cold water decyanation and the like; the secondary treatment mainly refers to the harmless treatment of phenol-cyanogen wastewater, mainly adopts an activated sludge method, and also comprises biological strengthening technologies, such as a biological iron method, a auxin adding method, a strengthening aeration method and the like; the three-stage deep treatment is secondary deep purification adopted when the drainage after biochemical treatment still can not reach the discharge standard, and the main processes of the three-stage deep treatment are an activated carbon adsorption method, a carbon-biofilm method, a coagulating sedimentation method and an oxidation pond method. More complicated pretreatment and other methods are adopted to control the water quality entering the biochemical system before the secondary biochemical treatment abroad, so as to prevent the concentration of toxic pollutants from being too high, and a three-level purification system is adopted after the biochemical treatment process.
The waste water after advanced treatment also produces a large proportion of high-salinity concentrated water while obtaining most of primary pure water, the high-salinity concentrated water has high pollutant concentration and high salinity, the direct discharge cannot reach the discharge standard, the conventional biochemical treatment difficulty is high, the prior concentrated water is used for flushing slag, but the concentrated water is easy to corrode and scale the pipelines and nozzles of equipment, and some enterprises adopt an evaporation crystallization method to treat the concentrated water, but the method has high equipment investment and operation cost. Therefore, the reduction of the coking wastewater is the key of the coking wastewater treatment.
Moreover, with the stricter and stricter environmental requirements, the call for zero discharge of wastewater from a coking plant is higher and higher, and the reduction treatment of the coking wastewater is a hotspot and a difficulty of the current research; the method has the advantages of good treatment effect, simple process flow, stable operation and reasonable cost, and has important practical significance on final zero discharge of coking wastewater and sustainable development of coking enterprises.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a coking wastewater reduction treatment method. The treatment effect is good and stable, the purposes of reduction treatment and resource utilization of the coking wastewater are finally achieved, and the method has important significance for realizing green ecological development of iron and steel enterprises.
In order to achieve the purpose, the invention adopts the following technical scheme:
a treatment method for reducing coking wastewater is used for treating coking ammonia distillation wastewater of steel enterprises, wherein suspended matters are 80 mg/L-100 mg/L, ammonia nitrogen is 60 mg/L-120 mg/L, phenol is 400 mg/L-500 mg/L, petroleum is 40 mg/L-50 mg/L, COD is 4000 mg/L-5000 mg/L, and total cyanide is 30 mg/L-80 mg/L.
The method specifically comprises the following steps:
1. the coking ammonia distillation wastewater firstly enters an adjusting tank to adjust the water quality and the water quantity, the effluent enters an air floatation oil removal device, the front end of the air floatation device adopts an aeration air floatation method, and 20mg/L to 30mg/L of Cationic Polyacrylamide (CPAM) and 30mg/L to 50mg/L of ZnSO are added4Aerating for 20-30 min, and standing for 30-40 min.
2. The supernatant enters a rear-end high-efficiency shallow ion air flotation tank, and 40-50 mg/L of coagulant FeSO is added at an inlet410 mg/L-20 mg/L coagulant aid Anion Polyacrylamide (APAM), the retention time is set to 10 min-15 min, after fully mixing and flocculating, the scum flows to a scum tank automatically through a spiral scum collecting device, the treated water enters a terminal settling zone, a series of shallow layers of settling layers are divided by inclined parallel pipes by adopting an inclined pipe settling method, and precipitates move and are separated from each other in each settling shallow layer to achieve the aim of settling.
3. Depositing for 40-50 min, allowing the clarified water to flow out by gravity and enter a biochemical homogenizing tank, lifting the homogenized and metered wastewater into a V-shaped biological filter by a pump, wherein a filter material is modified steel slag and has a particle size of 50-60 mm;
4. the effluent enters a secondary sedimentation tank for mud-water separation, and the retention time is 20-30 min;
5. the effluent water flows through the pipeline type UV at the flow velocity of 4-7 m/s by the pump, the wavelength range of the ultraviolet ray is 200-275 nm, and then the effluent water enters the ozone contact tower to react for 10-15 min by the pressurization of the jet pump.
6. The gas-liquid mixture after the rapid reaction flows into the degassing tower from the top of the contact tower through the pipeline pressure, the gas-liquid mixture is separated in the degassing tower, the gas upwards collects positive pressure discharge through the pipeline at the top of the degassing tower, and the liquid downwards collects positive pressure outflow through the pipeline at the bottom of the degassing tower, namely, the treated water is discharged.
7. The effluent enters a double-membrane treatment device with ultrafiltration and reverse osmosis, the produced water is recycled as industrial fresh water, the strong brine enters a chemical softening tank, 600 mg/L-800 mg/L calcium hydroxide and 300 mg/L-400 mg/L sodium carbonate are added, and the mixture is stirred for 10 min-20 min to remove scaling ions in the strong brine.
8. The effluent enters a sand filter tank for filtering, quartz sand is used as a filter material, the particle size is gradually reduced from bottom to top, the particle size of the lower layer of the filter material is 1.0 mm-1.5 mm, the particle size of the upper layer of the filter material is 0.5 mm-1.0 mm,
9. the filtered effluent enters ion exchange resin, wherein sodium type resin generated by the reaction of strong acid cation resin and NaCl can react with residual Ca in the solution2+、Mg2+And the cations are exchanged and adsorbed to be removed, so that the membrane pollution to the subsequent membrane treatment is reduced.
After the operation is carried out for a period of time, 3.0% -3.5% NaCl solution is used for regenerating the sodium chloride, regenerated wastewater flows back to the regulating reservoir, ion exchange resin produced water enters an ultrafiltration system, the pH value is regulated to 6.0-6.6 before entering a membrane unit, part of suspended matters and colloids in the wastewater can be removed through ultrafiltration, the SDI value of the ultrafiltration produced water is less than or equal to 3.0, the water inlet requirement of the nanofiltration membrane is met, and the recovery rate of the nanofiltration system is 95-98%.
10. And backwashing water of the ultrafiltration and nanofiltration membranes flows back to the front end regulating reservoir, nanofiltration produced water enters a bipolar membrane electrodialysis system, a bipolar membrane device consists of two bipolar membranes, two anion exchange membranes and one cation exchange membrane and is divided into 4 compartments, and salt in the water is converted into hydrochloric acid and sodium hydroxide, so that the reduction and resource utilization of the coking wastewater are realized.
Compared with the prior art, the invention has the beneficial effects that:
the invention provides a coking wastewater reduction treatment method, and the generated acid and alkali can be used for process recycling such as pH adjustment in the treatment process, so that the resource utilization of the coking wastewater is realized, the outsourcing cost of reagents is reduced, the energy consumption in the process is low, the cost is low, the equipment is simple, the operation is easy, the treatment effect is stable, and the treatment effect is enhanced by the water treatment reagent selected in the treatment process. The method realizes the reduction and resource utilization of the coking wastewater, and has important practical significance for the final zero discharge of the coking wastewater and the sustainable development of coking enterprises.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention discloses a coking wastewater reduction treatment method. Those skilled in the art can modify the process parameters appropriately to achieve the desired results with reference to the disclosure herein. It is expressly intended that all such similar substitutes and modifications which would be obvious to one skilled in the art are deemed to be included in the invention. While the methods and applications of this invention have been described in terms of preferred embodiments, it will be apparent to those of ordinary skill in the art that variations and modifications in the methods and applications described herein, as well as other suitable variations and combinations, may be made to implement and use the techniques of this invention without departing from the spirit and scope of the invention.
The treatment object of the invention is the coking ammonia distillation wastewater of steel enterprises, wherein suspended matters are 80 mg/L-100 mg/L, ammonia nitrogen is 60 mg/L-120 mg/L, phenol is 400 mg/L-500 mg/L, petroleum is 40 mg/L-50 mg/L, COD is 4000 mg/L-5000 mg/L, and total cyanide is 30 mg/L-80 mg/L.
The following description of the preferred embodiment of the present invention is provided in conjunction with FIG. 1:
example 1:
a coking wastewater reduction treatment method specifically comprises the following steps:
1. the coking ammonia distillation wastewater firstly enters an adjusting tank to adjust the water quality and the water quantity, the effluent enters an air floatation oil removal device, the front end of the air floatation device adopts an aeration air floatation method, and 20mg/L Cationic Polyacrylamide (CPAM) and 30mg/L ZnSO are added4Aerating for 20min, and standing for 30 min.
2. The supernatant fluid enters a rear-end high-efficiency shallow ion air flotation tank, and FeSO with 40mg/L of coagulant is added at the inlet4The coagulant aid is 10mg/L Anionic Polyacrylamide (APAM), the retention time is set to 10min, after full mixing and flocculation, scum automatically flows to a scum tank through a spiral scum collecting device, treated water enters a terminal settling zone, an inclined tube settling method is adopted, inclined parallel tubes are utilized to divide the scum tank into a series of shallow layers of settling layers, and precipitates move and are separated from each other in each settling shallow layer to achieve the purpose of settling.
3. And (3) allowing clarified water after 40min of precipitation to flow out by gravity and enter a biochemical homogenizing tank, lifting the homogenized and metered wastewater into a V-shaped biological filter by a pump, wherein a filter material is modified steel slag and has a particle size of 50 mm.
4. And (4) allowing the effluent to enter a secondary sedimentation tank for sludge-water separation, wherein the retention time is set to be 20 min.
5. The effluent water flows through the pipeline type UV at the flow rate of 4m/s by a pump, the wavelength range of the ultraviolet light is 275nm, and then the effluent water enters the ozone contact tower to react for 10min by the pressurization of a jet pump.
6. The gas-liquid mixture after the rapid reaction flows into the degassing tower from the top of the contact tower through the pipeline pressure, the gas-liquid mixture is separated in the degassing tower, the gas upwards collects positive pressure discharge through the pipeline at the top of the degassing tower, and the liquid downwards collects positive pressure outflow through the pipeline at the bottom of the degassing tower, namely, the treated water is discharged.
7. And (3) enabling the effluent to enter an ultrafiltration and reverse osmosis double-membrane treatment device, recycling the produced water as industrial fresh water, enabling the concentrated brine to enter a chemical softening tank, adding 600mg/L calcium hydroxide and 300mg/L sodium carbonate, and stirring for 10min to remove scaling ions in the concentrated brine.
8. Effluent enters a sand filter tank for filtering, quartz sand is used as a filter material, the particle size is gradually reduced from bottom to top and is placed, the particle size of the lower layer of the filter material is 1.0mm, and the particle size of the upper layer of the filter material is 0.5mm, so that suspended matters are further removed.
9. The filtered effluent enters ion exchange resin, wherein sodium type resin generated by the reaction of strong acid cation resin and NaCl can react with residual Ca in the solution2+、Mg2+And the cations are exchanged and adsorbed to be removed, so that the membrane pollution to the subsequent membrane treatment is reduced. After the operation for a period of time, the wastewater is regenerated by using 3.0% NaCl solution, the regenerated wastewater flows back to the regulating reservoir, the ion exchange resin produced water enters the ultrafiltration system, the pH value is regulated to 6.0 before entering the membrane unit, partial suspended matters and colloids in the wastewater can be removed by ultrafiltration, the SDI value of the ultrafiltration produced water is 3.0, the water inlet requirement of the nanofiltration membrane is met, and the recovery rate of the nanofiltration system is 95%.
10. And the backwashing water of the ultrafiltration and nanofiltration membranes flows back to the front end regulating tank. Nanofiltration produced water enters a bipolar membrane electrodialysis system, a bipolar membrane device consists of two bipolar membranes, two anion exchange membranes and one cation exchange membrane and is divided into 4 compartments, and salt in the water is converted into hydrochloric acid and sodium hydroxide, so that the reduction and resource utilization of the coking wastewater are realized.
Example 2:
a coking wastewater reduction treatment method specifically comprises the following steps:
1. the coking ammonia distillation wastewater firstly enters an adjusting tank to adjust the water quality and the water quantity, the effluent enters an air floatation oil removal device, the front end of the air floatation device adopts an aeration air floatation method, and 25mg/L Cationic Polyacrylamide (CPAM) and 40mg/L ZnSO are added4Aerating for 25min, and standing for 35 min.
2. The supernatant fluid enters a rear-end high-efficiency shallow ion air flotation tank, and FeSO with a coagulant of 45mg/L is added at the inlet4The coagulant aid is 15mg/L Anionic Polyacrylamide (APAM), the retention time is set to be 13min, after full mixing and flocculation, scum automatically flows to a scum tank through a spiral scum collecting device, treated water enters a terminal settling zone, an inclined tube settling method is adopted, inclined parallel tubes are utilized to divide the scum tank into a series of shallow layers of settling layers, and precipitates move and are separated from each other in each settling shallow layer to achieve the purpose of settling.
3. And (3) allowing clear water after 45min of precipitation to flow out by gravity and enter a biochemical homogenizing tank, lifting the homogenized and metered waste water into a V-shaped biological filter by a pump, wherein a filter material is modified steel slag and has a particle size of 55 mm.
4. And (4) allowing the effluent to enter a secondary sedimentation tank for mud-water separation, wherein the retention time is set to be 25 min.
5. The effluent water flows through the pipeline type UV at the flow rate of 5m/s by a pump, the wavelength range of the ultraviolet light is 275nm, and then the effluent water enters the ozone contact tower to react for 13min by the pressurization of a jet pump.
6. The gas-liquid mixture after the rapid reaction flows into the degassing tower from the top of the contact tower through the pipeline pressure, the gas-liquid mixture is separated in the degassing tower, the gas upwards collects positive pressure discharge through the pipeline at the top of the degassing tower, and the liquid downwards collects positive pressure outflow through the pipeline at the bottom of the degassing tower, namely, the treated water is discharged.
7. And (3) enabling the effluent to enter an ultrafiltration and reverse osmosis double-membrane treatment device, recycling the produced water as industrial fresh water, enabling the concentrated brine to enter a chemical softening tank, adding 700mg/L calcium hydroxide and 350mg/L sodium carbonate, and stirring for 15min to remove scaling ions in the concentrated brine.
8. Effluent enters a sand filter tank for filtering, quartz sand is used as a filter material, the particle size is gradually reduced from bottom to top and is placed, the particle size of the lower layer of the filter material is 1.3mm, and the particle size of the upper layer of the filter material is 0.8mm, so that suspended matters are further removed.
9. The filtered effluent enters ion exchange resin, wherein sodium type resin generated by the reaction of strong acid cation resin and NaCl can react with residual Ca in the solution2+、Mg2+The cations are subjected to exchange adsorption so as to be removed, membrane pollution to subsequent membrane treatment is reduced, after the membrane treatment device is operated for a period of time, 3.2% NaCl solution is used for regenerating the cations, regenerated wastewater flows back to the regulating tank, ion exchange resin produced water enters an ultrafiltration system, the pH value is regulated to 6.3 before entering a membrane unit, partial suspended matters and colloid in the wastewater can be removed by ultrafiltration, the SDI value of the ultrafiltration produced water is 2.8, the water inlet requirement of the nanofiltration membrane is met, and the recovery rate of the nanofiltration system is 96%.
10. And the backwashing water of the ultrafiltration and nanofiltration membranes flows back to the front end regulating tank. Nanofiltration produced water enters a bipolar membrane electrodialysis system, a bipolar membrane device consists of two bipolar membranes, two anion exchange membranes and one cation exchange membrane and is divided into 4 compartments, and salt in the water is converted into hydrochloric acid and sodium hydroxide, so that the reduction and resource utilization of the coking wastewater are realized.
Example 3:
a coking wastewater reduction treatment method specifically comprises the following steps:
1. the coking ammonia distillation wastewater firstly enters an adjusting tank to adjust the water quality and the water quantity, the effluent enters an air floatation oil removal device, the front end of the air floatation device adopts an aeration air floatation method, and 30mg/L Cationic Polyacrylamide (CPAM) and 50mg/L ZnSO are added4Aerating for 30min, and standing for 40 min.
2. The supernatant fluid enters a rear-end high-efficiency shallow ion air flotation tank, and FeSO with coagulant of 50mg/L is added at the inlet4The coagulant aid is Anionic Polyacrylamide (APAM) with 20mg/L, the retention time is set to be 15min, after full mixing and flocculation, scum automatically flows to a scum pond through a spiral scum collecting device, treated water enters a terminal settling zone, an inclined tube settling method is adopted, and a series of shallow layers are divided by inclined parallel tubesAnd (4) a sediment layer, wherein sediments move mutually and are separated in each shallow sediment layer, so that the purpose of sedimentation is achieved.
3. And (3) allowing clear water after 50min of precipitation to flow out by gravity and enter a biochemical homogenizing tank, lifting the homogenized and metered waste water into a V-shaped biological filter by a pump, wherein a filter material is modified steel slag and has a particle size of 60 mm.
4. And (4) allowing the effluent to enter a secondary sedimentation tank for sludge-water separation, wherein the retention time is set to be 30 min.
5. The effluent water flows through the pipeline type UV at the flow rate of 7m/s by a pump, the wavelength range of the ultraviolet light is 275nm, and then the effluent water enters the ozone contact tower to react for 15min by pressurizing by a jet pump.
6. The gas-liquid mixture after the rapid reaction flows into the degassing tower from the top of the contact tower through the pipeline pressure, the gas-liquid mixture is separated in the degassing tower, the gas upwards collects positive pressure discharge through the pipeline at the top of the degassing tower, and the liquid downwards collects positive pressure outflow through the pipeline at the bottom of the degassing tower, namely, the treated water is discharged.
7. And (3) enabling the effluent to enter an ultrafiltration and reverse osmosis double-membrane treatment device, recycling the produced water as industrial fresh water, enabling the concentrated brine to enter a chemical softening tank, adding 800mg/L calcium hydroxide and 400mg/L sodium carbonate, and stirring for 20min to remove scaling ions in the concentrated brine.
8. Effluent enters a sand filter tank for filtering, quartz sand is used as a filter material, the particle size is gradually reduced from bottom to top and is placed, the particle size of the lower layer of the filter material is 1.5mm, and the particle size of the upper layer of the filter material is 1.0mm, so that suspended matters are further removed.
9. The filtered effluent enters ion exchange resin, wherein sodium type resin generated by the reaction of strong acid cation resin and NaCl can react with residual Ca in the solution2+、Mg2+The cations are exchanged and adsorbed to be removed, membrane pollution to subsequent membrane treatment is reduced, after the membrane treatment is carried out for a period of time, 3.5% NaCl solution is used for regenerating the cations, regenerated wastewater flows back to the regulating reservoir, ion exchange resin produced water enters the ultrafiltration system, the pH value is regulated to 6.6 before entering the membrane unit, partial suspended matters and colloid in the wastewater can be removed by ultrafiltration, the SDI value of the ultrafiltration produced water is 2.5, the water inlet requirement of the nanofiltration membrane is met, and the recovery rate of the nanofiltration system is 98%.
10. And the backwashing water of the ultrafiltration and nanofiltration membranes flows back to the front end regulating tank. Nanofiltration produced water enters a bipolar membrane electrodialysis system, a bipolar membrane device consists of two bipolar membranes, two anion exchange membranes and one cation exchange membrane and is divided into 4 compartments, and salt in the water is converted into hydrochloric acid and sodium hydroxide, so that the reduction and resource utilization of the coking wastewater are realized.
The acid and alkali generated by the invention can be used for process recycling such as pH adjustment in the treatment process, so that the resource utilization of the coking wastewater is realized, the outsourcing cost of reagents is reduced, the energy consumption in the process is low, the cost is low, the equipment is simple, the operation is easy, the treatment effect is stable, and the water treatment agent selected in the treatment process enhances the treatment effect. The method realizes the reduction and resource utilization of the coking wastewater, and has important practical significance for the final zero discharge of the coking wastewater and the sustainable development of coking enterprises.
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 (7)
1. A coking wastewater reduction treatment method is characterized in that the coking wastewater is coking ammonia distillation wastewater of steel enterprises, wherein suspended matters are 80 mg/L-100 mg/L, ammonia nitrogen is 60 mg/L-120 mg/L, phenol is 400 mg/L-500 mg/L, petroleum is 40 mg/L-50 mg/L, COD is 4000 mg/L-5000 mg/L, and total cyanide is 30 mg/L-80 mg/L; the method specifically comprises the following steps:
1) firstly, feeding the coking ammonia distillation wastewater into an adjusting tank to adjust the water quality and the water quantity, feeding the effluent into an air flotation oil removal device, wherein the front end of the air flotation device adopts an aeration air flotation method, and adding 20-30 mg/L cationic polyacrylamide and 30-50 mg/L ZnSO4Aerating for 20-30 min, and standing for 30-40 min;
2, enabling the supernatant to enter a rear-end high-efficiency shallow ion air flotation tank, adding a coagulant and a coagulant aid at an inlet, staying for 10-15 min, fully mixing and flocculating, enabling scum to automatically flow to a scum tank through a spiral scum collecting device, and enabling treated water to enter a terminal settling zone;
3) depositing for 40-50 min, and allowing the clarified water to flow out by gravity and enter a biochemical homogenizing tank, and lifting the homogenized wastewater by a pump and then entering a V-shaped biological filter for filtering;
4) the effluent enters a secondary sedimentation tank for mud-water separation, and stays for 20-30 min;
5) the effluent water flows through the pipeline type UV at the flow velocity of 4-7 m/s by a pump, the wavelength range of the ultraviolet ray is 200-275 nm, and then the effluent water enters an ozone contact tower to react for 10-15 min by the pressurization of a jet pump;
6) the reacted gas-liquid mixture flows into a degassing tower from the top of a contact tower through pipeline pressure, the gas-liquid mixture is separated in the degassing tower, the gas is discharged upwards through positive pressure collected by a pipeline at the top of the degassing tower, and the liquid flows downwards through a pipeline at the bottom of the degassing tower and is collected by positive pressure, namely treated effluent;
7) the effluent enters a double-membrane treatment device with ultrafiltration and reverse osmosis, the produced water is recycled as industrial fresh water, strong brine enters a chemical softening tank, 600-800 mg/L calcium hydroxide and 300-400 mg/L sodium carbonate are added, and the mixture is stirred for 10-20 min to remove scaling ions in the strong brine;
8) the effluent enters a sand filter tank for filtering, quartz sand is used as a filter material, the particle size is gradually reduced from bottom to top, the lower layer of the filter material has the particle size of 1.0-1.5 mm, and the upper layer of the filter material has the particle size of 0.5-1.0 mm, so that suspended matters are further removed;
9) the filtered effluent enters ion exchange resin, 3.0-3.5% NaCl solution is used for regenerating the effluent, the regenerated wastewater flows back to the regulating reservoir, the water produced by the ion exchange resin enters an ultrafiltration system, the pH value is regulated to 6.0-6.6 before entering a membrane unit, the SDI value of the ultrafiltration water is less than or equal to 3.0, and the recovery rate of the nanofiltration system is 95-98%;
10) the backwashing water of the ultrafiltration and nanofiltration membranes flows back to the front end regulating tank; and (4) the nanofiltration produced water enters a bipolar membrane electrodialysis system to convert the salt in the water into hydrochloric acid and sodium hydroxide.
2. The coking wastewater reduction method according to claim 1The treatment method is characterized in that the coagulant in the step 2) is FeSO with the concentration of 40 mg/L-50 mg/L4The coagulant aid is anionic polyacrylamide with the concentration of 10 mg/L-20 mg/L.
3. The coking wastewater reduction treatment method according to claim 1, characterized in that the settling zone of the step 2) is divided into a series of shallow settling layers by an inclined tube settling method by utilizing inclined parallel tubes, and sediments move and are separated from each other in each shallow settling layer to achieve the purpose of settling.
4. The coking wastewater reduction treatment method according to claim 1, characterized in that the V-shaped biofilter filter material in the step 3) is modified steel slag with a particle size of 50 mm-60 mm.
5. The coking wastewater reduction treatment method according to claim 1, characterized in that the sand filter tank in the step 8) adopts quartz sand as a filter material, the particle size of the filter material in the lower layer is gradually reduced from bottom to top, the particle size of the filter material in the lower layer is 1.0 mm-1.5 mm, and the particle size of the filter material in the upper layer is 0.5 mm-1.0 mm.
6. The coking wastewater reduction treatment method according to claim 1, characterized in that the ion exchange resin in the step 9) is a sodium resin formed by the reaction of a strong acid cation resin and NaCl.
7. The coking wastewater reduction treatment method according to claim 1, characterized in that the bipolar membrane device of the bipolar membrane electrodialysis system in the step 10) is composed of two bipolar membranes, two anion exchange membranes and one cation exchange membrane, and is divided into 4 compartments.
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| CN116553791A (en) * | 2023-07-07 | 2023-08-08 | 北京百灵天地环保科技股份有限公司 | Coking phenol-cyanogen wastewater advanced treatment process |
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| CN105800885A (en) * | 2016-05-23 | 2016-07-27 | 北京今大禹环境技术股份有限公司 | Resource recycling and treatment system of high-concentration degradation-resistant salt-containing organic waste water |
| CN111268859A (en) * | 2020-01-21 | 2020-06-12 | 鞍钢股份有限公司 | Method for simultaneously preparing hydrochloric acid and sodium hydroxide by utilizing reverse osmosis strong brine |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105800885A (en) * | 2016-05-23 | 2016-07-27 | 北京今大禹环境技术股份有限公司 | Resource recycling and treatment system of high-concentration degradation-resistant salt-containing organic waste water |
| CN111268859A (en) * | 2020-01-21 | 2020-06-12 | 鞍钢股份有限公司 | Method for simultaneously preparing hydrochloric acid and sodium hydroxide by utilizing reverse osmosis strong brine |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116553791A (en) * | 2023-07-07 | 2023-08-08 | 北京百灵天地环保科技股份有限公司 | Coking phenol-cyanogen wastewater advanced treatment process |
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