CN216550031U - Ammonia distillation, coal gas water seal, rainwater and sludge filtrate mixed wastewater treatment system - Google Patents
Ammonia distillation, coal gas water seal, rainwater and sludge filtrate mixed wastewater treatment system Download PDFInfo
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- CN216550031U CN216550031U CN202123138929.5U CN202123138929U CN216550031U CN 216550031 U CN216550031 U CN 216550031U CN 202123138929 U CN202123138929 U CN 202123138929U CN 216550031 U CN216550031 U CN 216550031U
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Abstract
The utility model provides a system for treating mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate. The device comprises a gas water seal primary sedimentation tank, a gravity oil separation tank, a mixed air floatation oil removal tank, a rainwater lifting well, an adjusting tank, a primary aerator tank, a primary sedimentation tank, an accident tank, an oil collecting tank, an anaerobic tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank and the like. The utility model organically combines pretreatment, biochemical treatment and advanced treatment, adopts an MBBR biological fluidized bed process, occupies less land, only needs 20 percent of the volume of a common oxidation pond under the same load condition, and microorganisms are attached to carriers to flow along with water flow without active sludge backflow or circulating back washing, and simultaneously the carrier organisms continuously fall off to avoid blockage, and has high organic load, strong impact load resistance and stable effluent quality. The utility model has the advantages of small head loss, low power consumption, simple operation and easy operation and management, and is suitable for new construction and reconstruction projects.
Description
Technical Field
The utility model relates to the field of environmental protection, in particular to the field of industrial wastewater treatment, and particularly relates to a system for treating mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate.
Background
In the steel and coking industry, a large amount of waste water with complex chemical components, difficult biodegradation, toxicity and harm such as ammonia evaporation waste water, coal gas water seal waste water and the like is generated, the waste water, rainwater and sludge filtrate are mixed and then treated by the enterprises, and the expected treatment effect cannot be achieved by a simple biochemical treatment method.
SUMMERY OF THE UTILITY MODEL
According to the technical problems, the system and the method for treating the mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate are provided. The main trend of realizing standard treatment of the industrial wastewater difficult to degrade at present is to supplement physicochemical treatment on the basis of a biochemical treatment method. The combination of various process units can improve the biodegradability of the wastewater, effectively save energy and reduce investment and operation cost. The technical means adopted by the utility model are as follows:
a mixed wastewater treatment system of ammonia still, gas water seal, rainwater and sludge filtrate comprises a gas water seal primary sedimentation tank, a gravity oil separation tank, a mixed air flotation oil removal tank, a rainwater lifting well, a regulating tank, a primary aeration tank, a primary sedimentation tank, an accident tank, an oil collecting tank, an anaerobic tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, an intermediate water tank, a biochemical sludge concentration tank, an MBBR biological fluidized bed, a mechanical coagulation reaction tank, a coagulation sedimentation tank, a reuse water tank and a physicochemical sludge concentration tank,
the ammonia evaporation wastewater is connected with a water inlet of a gravity oil separation tank, gas water seal water is connected with a water inlet of a gas water seal water primary sedimentation tank, a water outlet of the gas water seal water primary sedimentation tank is connected with the gravity oil separation tank, a water outlet of the gravity oil separation tank is connected with a mixed air floatation oil removal tank, rainwater and sludge filtrate are collected to a rainwater lift well, a water outlet of the rainwater lift well and a water outlet of the air floatation oil removal tank are both connected with a water inlet of an adjusting tank, a water outlet of the adjusting tank is connected with a water inlet of a primary aeration tank, and a water outlet of the primary aeration tank is connected with the primary sedimentation tank; the water outlet of the primary sedimentation tank is connected with the anaerobic tank, the water outlet of the anaerobic tank is connected with the anoxic tank, the water outlet of the anoxic tank is connected with the aerobic tank, the water outlet of the aerobic tank is respectively connected with the anoxic tank and the secondary sedimentation tank, one part of biochemical residual sludge generated by the secondary sedimentation tank flows back to the primary sedimentation tank and the anoxic tank, and the other part of biochemical residual sludge is discharged to the biochemical sludge concentration tank; the wastewater after the biochemical treatment of the secondary sedimentation tank enters an MBBR biological fluidized bed through an intermediate water tank, the MBBR biological fluidized bed is connected with a mechanical coagulation reaction tank, the mechanical coagulation reaction tank is connected with a coagulation sedimentation tank, the coagulation sedimentation tank is connected with a reuse water tank, the coagulation sedimentation tank is also connected with a materialized sludge concentration tank, and the materialized sludge concentration tank is connected with the mechanical coagulation reaction tank;
and (3) the accident water enters the accident pool, the water outlet of the accident pool is connected with the water inlet of the gravity oil separation pool, and the waste oil generated by the gravity oil separation pool and the mixed air floatation oil removal pool is connected with the oil collection pool.
Furthermore, the aerobic tank comprises a first aerobic tank and a second aerobic tank, the water outlet of the anoxic tank is connected with the first aerobic tank, the first aerobic tank is connected with the second aerobic tank, and nitrified liquid in the first aerobic tank and the second aerobic tank flows back to the anoxic tank at the front section of the process.
Further, the biochemical sludge concentration tank is connected with the first screw dehydrator, the first screw dehydrator is dehydrated until the water content is less than 80%, the blended coal is burnt, and supernatant generated by the first screw dehydrator flows back to the rainwater lifting well.
Further, a Fenton reagent is added into the mechanical coagulation reaction tank.
And further, the materialized sludge concentration tank is connected with a second screw-stacking dehydrator, the second screw-stacking dehydrator is dehydrated until the water content is less than 80%, coal blending combustion or outward transportation centralized treatment is carried out, and supernate generated by the materialized sludge concentration tank flows back to the mechanical coagulation reaction tank for reprecipitation.
Further, the second spiral shell stacking dehydrator is connected with the first spiral shell stacking dehydrator.
Further, the treated wastewater of the reuse water tank is used as water for flushing slag and defoaming phenol-cyanogen sewage in a steel mill.
A method for treating mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate comprises the following steps:
step 1, ammonia evaporation wastewater and gas water seal water contain a large amount of floating oil, the ammonia evaporation wastewater enters a gravity oil separation tank through a water inlet pipeline, the gas water seal water automatically flows into the gravity oil separation tank after being precipitated in a gas water seal primary sedimentation tank, and the ammonia evaporation wastewater and the gas water seal water are mixed in the gravity oil separation tank; accident water enters an accident pool for temporary storage and is conveyed to a gravity oil separation pool for treatment;
and 5, in the anoxic tank, denitrifying bacteria take organic matters in the wastewater as a carbon source, carry a large amount of nitrate nitrogen and nitrite nitrogen into the reflux mixed solution, reduce the nitrate nitrogen and the nitrite nitrogen into nitrogen and release the nitrogen to the air, wherein the anoxic tank is used for enabling BOD in the sewage to be in the anoxic tank5The concentration is reduced, and the nitrogen concentration of the nitrate is greatly reduced;
step 7, enabling the wastewater to automatically flow into a secondary sedimentation tank through a second aerobic tank, enabling one part of biochemical residual sludge generated by the secondary sedimentation tank to flow back to a primary sedimentation tank and an anoxic tank, discharging the other part of biochemical residual sludge to a biochemical sludge concentration tank, dehydrating through a first spiral shell stacking dehydrator until the water content is less than 80%, blending coal for combustion, enabling supernatant generated by the first spiral shell stacking dehydrator to flow back to a rainwater lifting well, pumping to a regulating tank, and performing biochemical treatment again;
8, enabling the biochemically treated wastewater to automatically flow into a middle water tank, conveying the wastewater to an MBBR (moving bed biofilm reactor) biological fluidized bed through a water pump, performing further nitration reaction and denitrification reaction, enabling the mixed wastewater to automatically flow into a mechanical coagulation reaction tank, then automatically flow into a coagulation sedimentation tank for flocculation sedimentation reaction, then automatically flow into a reuse water tank, enabling the effluent to be used for slag flushing and defoaming water of a steel mill, enabling the materialized sludge generated in the coagulation sedimentation tank to enter a materialized sludge concentration tank for concentration, dehydrating the materialized sludge until the water content is less than 80% through a second spiral dehydrator, carrying out outward transportation centralized treatment, and enabling supernatant generated in the materialized sludge concentration tank to flow back to the mechanical coagulation reaction tank for reprecipitation; wherein, Fenton reagent is added into the mechanical coagulation reaction tank.
The utility model has the following advantages:
1. the process method organically combines pretreatment, biochemical treatment and advanced treatment, adopts an MBBR biological fluidized bed process, occupies less land, only needs 20 percent of the volume of a common oxidation pond under the same load condition, and microorganisms are attached to carriers to flow along with water flow, so that active sludge backflow or circulating back washing is not needed, and simultaneously carrier organisms continuously fall off to avoid blockage, and the process method has high organic load, strong impact load resistance and stable effluent quality;
2. compared with the conventional dosing coagulating sedimentation process, the Fenton strong oxidation process has obvious removal effect on benzene, polycyclic and heterocyclic toxic substances, and the Fenton oxidant has good degradation effect on benzene series substances such as benzene, toluene and ethylbenzene according to the Fenton oxidation method styrene device wastewater treatment (2014) experiment, and the removal rate is more than 90%;
3. the method has the advantages of small head loss, low power consumption, simple operation and easy operation and management, and is suitable for new construction and reconstruction projects.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a flow chart of the treatment process of the mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in figure 1, the utility model discloses a system for treating mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate, which comprises a gravity oil separation tank 1, a mixed air flotation oil removal tank 2, an adjusting tank 3, a primary exposure tank 4, a primary sedimentation tank 5, an anaerobic tank 6, an anoxic tank 7, a first aerobic tank 8, a second aerobic tank 9, a secondary sedimentation tank 10, a middle water tank 11, an MBBR biological fluidized bed 12, a mechanical coagulation reaction tank 13, a coagulation sedimentation tank 14, a reuse water tank 15, an accident tank 16, an oil collecting tank 17, a gas water seal primary sedimentation tank 18, a rainwater lifting well 19, a first spiral dehydrator 20, a biochemical sludge concentration tank 21, a second spiral dehydrator 22 and a physicochemical sludge concentration tank 23.
The working process of the utility model is as follows:
the ammonia evaporation wastewater and the gas water seal water contain a large amount of floating oil, the ammonia evaporation wastewater enters a gravity oil separation tank through a water inlet pipeline, the gas water seal water automatically flows into the gravity oil separation tank after being precipitated by a gas water seal primary sedimentation tank, the gas water seal water and the gas water seal water are mixed in the gravity oil separation tank, the mixed wastewater is subjected to oil separation and oil removal treatment by the gravity oil separation tank and a mixed air flotation oil removal tank, and then enters an adjusting tank together with initial rainwater and sludge filtrate through a rainwater lifting well for homogenization treatment, the mixed wastewater after homogenization enters a primary exposure tank with long residence time for removing phenols and cyanides, and the mixed wastewater automatically flows into the primary sedimentation tank for primary sedimentation. The accident water enters an accident pool for temporary storage and is sent to a gravity oil separation pool for treatment through a pump with small flow and multiple times, the process is generally called as a pretreatment process, and the effluent water and COD in the processcrThe removal rate is more than or equal to 65 percent, the removal rate of volatile phenol is more than or equal to 99.89 percent, the removal rate of cyanide is more than or equal to 97.50 percent, the removal rate of petroleum is more than or equal to 98.35 percent, and the removal rate of sulfide is more than or equal to 57.00 percent. Waste oil produced by gravity oil separation tank and mixed air-float oil-removing tank belongs to dangerous waste material, and its code is that in HW11 rectification residue252 and 011-11, the generated waste oil automatically flows into an oil collecting pool and is entrusted to a qualified professional unit for disposal.
The pretreated wastewater automatically flows into an anaerobic tank, and in the anaerobic tank, the wastewater releases phosphorus, so that the concentration of the phosphorus in the wastewater is increased, and soluble organic matters are absorbed by microbial cells to ensure that BOD (biochemical oxygen demand) in the wastewater is increased5The concentration decreases and part of nitrogen in the nitrate is removed by cell synthesis, thereby decreasing nitrate nitrogen in the wastewater. The wastewater automatically flows into an anoxic tank through an anaerobic tank, in the anoxic tank, denitrifying bacteria utilize organic matters in the wastewater as carbon sources to carry a large amount of nitrate nitrogen and nitrite nitrogen into the reflux mixed liquid and reduce the nitrate nitrogen into nitrogen to be released to the air, so that BOD (biochemical oxygen demand) is achieved5The concentration is reduced, the nitrogen concentration of the nitrate is greatly reduced, and the change of phosphorus is small. The wastewater automatically flows into a first aerobic tank and a second aerobic tank through an anoxic tank, sodium carbonate or sodium hydroxide is added into the first aerobic tank, organic matters in the wastewater are biochemically degraded by microorganisms and continuously descend in the first aerobic tank and the second aerobic tank, organic nitrogen is aminated and then nitrified, the concentration of ammonia nitrogen is obviously reduced, the concentration of nitrate nitrogen is increased along with nitrification, and phosphorus is also reduced at a higher speed along with excessive uptake of phosphorus-accumulating bacteria. Nitrifying liquid in the second aerobic pool at the rear section flows back to the anoxic pool at the front section of the process, the nitrifying liquid contains nitrate nitrogen generated by oxidizing ammonia nitrogen by nitrifying bacteria, and the nitrate nitrogen can be mixed with organic matters in inlet water in the anaerobic pool or the anoxic pool after flowing back to the front end, and denitrification of the nitrate nitrogen is carried out by denitrifying bacteria, so that total nitrogen removal is realized. Waste water gets into two heavy ponds through second good oxygen pond autonomous flow, and two biochemical excess sludge that heavy pond produced partly passes through the pump and carries backward flow to just sinking pond and oxygen deficiency pond, and the effect is the activated sludge who supplies aeration tank mixed liquid outflow to take away, makes suspended solid concentration MLSS in the aeration tank keep relatively stable, and when mud backward flow, increases the stirring in the pond simultaneously, makes the contact of mud and sewage even, can improve sewage treatment effect, also can play certain effect to the quality of water of buffering intaking simultaneously. The other part is discharged to a biochemical sludge concentration tank, and is dehydrated by a first spiral shell stacking dehydrator until the water content is less than 80 percent, the blended coal is burnt, and the supernatant generated by the first spiral shell stacking dehydratorAnd returning the liquid to the rainwater lifting well, pumping the liquid to a regulating reservoir for biochemical treatment, wherein the process is generally called a biochemical treatment process. The removal rate of CODcr of effluent produced in the process is not less than 91.50%, the removal rate of ammonia nitrogen is not less than 83.50%, the removal rate of volatile phenol is not less than 85.00%, and the removal rate of sulfide is not less than 91.80%.
The wastewater after biochemical treatment automatically flows into an intermediate water tank, the wastewater is conveyed to an MBBR biological fluidized bed through a water pump for further nitration reaction and denitrification reaction, the mixed wastewater automatically flows into a mechanical coagulation reaction tank, then automatically flows into a coagulation sedimentation tank for flocculation and precipitation reaction, and then automatically flows into a reuse water tank, the effluent is used for slag flushing and defoaming water of a steel mill, the materialized sludge generated in the coagulation sedimentation tank enters a materialized sludge concentration tank for concentration, the materialized sludge is dehydrated to the water content of less than 80% through a second spiral dehydrator and is transported out for centralized treatment, the supernatant generated in the materialized sludge concentration tank flows back to the mechanical coagulation reaction tank for reprecipitation, and a Fenton reagent is added into the mechanical coagulation reaction tank for further removing pollutants. This process is commonly referred to as a deep processing process. The CODcr removal rate of effluent produced in the process is more than or equal to 73.50 percent, the ammonia nitrogen removal rate is more than or equal to 90.50 percent, the cyanide removal rate is more than or equal to 60.00 percent, and the sulfide removal rate is more than or equal to 85.70 percent. The second spiral shell dehydrator is connected with the first spiral shell dehydrator, and the second spiral shell dehydrator plays a role in mutual standby, and if one spiral shell dehydrator breaks down, the sludge-containing sewage can be conveyed to the other spiral shell dehydrator for dehydration, so that the operation of the whole water treatment system is not influenced.
The effluent meets the discharge standard of pollutants for coking chemical industry (GB16171-2012) Table 2, namely CODcrLess than or equal to 80mg/L, less than or equal to 0.30mg/L of volatile phenol, less than or equal to 10mg/L of ammonia nitrogen, less than or equal to 0.20mg/L of cyanide, less than or equal to 2.5mg/L of petroleum and less than or equal to 0.50mg/L, pH of sulfide, and the treated wastewater can be used as slag flushing water in steel mills and water for defoaming phenol-cyanogen sewage.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the utility model has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (7)
1. A mixed wastewater treatment system of ammonia still, gas water seal, rainwater and sludge filtrate is characterized by comprising a gas water seal primary sedimentation tank, a gravity oil separation tank, a mixed air flotation oil removal tank, a rainwater lifting well, an adjusting tank, a primary aeration tank, a primary sedimentation tank, an accident tank, an oil collection tank, an anaerobic tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a middle water tank, a biochemical sludge concentration tank, an MBBR biological fluidized bed, a mechanical coagulation reaction tank, a coagulation sedimentation tank, a reuse water tank and a physicochemical sludge concentration tank,
the ammonia evaporation wastewater is connected with a water inlet of a gravity oil separation tank, gas water seal water is connected with a water inlet of a gas water seal water primary sedimentation tank, a water outlet of the gas water seal water primary sedimentation tank is connected with the gravity oil separation tank, a water outlet of the gravity oil separation tank is connected with a mixed air floatation oil removal tank, rainwater and sludge filtrate are collected to a rainwater lift well, a water outlet of the rainwater lift well and a water outlet of the air floatation oil removal tank are both connected with a water inlet of an adjusting tank, a water outlet of the adjusting tank is connected with a water inlet of a primary aeration tank, and a water outlet of the primary aeration tank is connected with the primary sedimentation tank; the water outlet of the primary sedimentation tank is connected with the anaerobic tank, the water outlet of the anaerobic tank is connected with the anoxic tank, the water outlet of the anoxic tank is connected with the aerobic tank, the water outlet of the aerobic tank is respectively connected with the anoxic tank and the secondary sedimentation tank, one part of biochemical residual sludge generated by the secondary sedimentation tank flows back to the primary sedimentation tank and the anoxic tank, and the other part of biochemical residual sludge is discharged to the biochemical sludge concentration tank; the wastewater after the biochemical treatment of the secondary sedimentation tank enters an MBBR biological fluidized bed through an intermediate water tank, the MBBR biological fluidized bed is connected with a mechanical coagulation reaction tank, the mechanical coagulation reaction tank is connected with a coagulation sedimentation tank, the coagulation sedimentation tank is connected with a reuse water tank, the coagulation sedimentation tank is also connected with a materialized sludge concentration tank, and the materialized sludge concentration tank is connected with the mechanical coagulation reaction tank;
and (3) the accident water enters the accident pool, the water outlet of the accident pool is connected with the water inlet of the gravity oil separation pool, and the waste oil generated by the gravity oil separation pool and the mixed air floatation oil removal pool is connected with the oil collection pool.
2. The system for treating wastewater mixed by ammonia distillation, gas water seal, rainwater and sludge filtrate according to claim 1, wherein the aerobic tank comprises a first aerobic tank and a second aerobic tank, the water outlet of the anoxic tank is connected with the first aerobic tank, the first aerobic tank is connected with the second aerobic tank, and the nitrified liquid in the first aerobic tank and the nitrified liquid in the second aerobic tank flow back to the anoxic tank at the front section of the process.
3. The system for treating mixed wastewater of ammonia distillation, gas water seal, rainwater and sludge filtrate according to claim 1, wherein the biochemical sludge concentration tank is connected with the first screw dehydrator, the first screw dehydrator dehydrates until the water content is less than 80%, the coal blending is burned, and the supernatant generated by the first screw dehydrator flows back to the rainwater lifting well.
4. The ammonia still, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system according to claim 1, wherein a Fenton reagent is added into the mechanical coagulation reaction tank.
5. The system for treating the mixed wastewater of the ammonia still, the gas water seal, the rainwater and the sludge filtrate as claimed in claim 1 or 3, wherein the materialized sludge concentration tank is connected with the second screw dehydrator, the second screw dehydrator is used for dehydration until the water content is less than 80%, the coal blending or outward transportation is used for centralized treatment, and supernatant generated by the materialized sludge concentration tank flows back to the mechanical coagulation reaction tank for reprecipitation.
6. The ammonia still, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system according to claim 5, wherein the second screw-stacking dehydrator is connected with the first screw-stacking dehydrator.
7. The system for treating the mixed wastewater of the ammonia still, the gas water seal, the rainwater and the sludge filtrate as recited in claim 1, wherein the treated wastewater of the reuse water tank is used as water for flushing slag of steel mills and defoaming phenol-cyanogen sewage.
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| CN202123138929.5U CN216550031U (en) | 2021-12-13 | 2021-12-13 | Ammonia distillation, coal gas water seal, rainwater and sludge filtrate mixed wastewater treatment system |
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| CN202123138929.5U CN216550031U (en) | 2021-12-13 | 2021-12-13 | Ammonia distillation, coal gas water seal, rainwater and sludge filtrate mixed wastewater treatment system |
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| CN216550031U true CN216550031U (en) | 2022-05-17 |
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