CN113772892A - Coking wastewater and domestic sewage combined treatment system and treatment method - Google Patents
Coking wastewater and domestic sewage combined treatment system and treatment method Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 79
- 238000004939 coking Methods 0.000 title claims abstract description 60
- 239000010865 sewage Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 307
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 146
- 238000004062 sedimentation Methods 0.000 claims abstract description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 46
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 19
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 230000001112 coagulating effect Effects 0.000 claims abstract description 14
- 230000009615 deamination Effects 0.000 claims abstract description 5
- 238000006481 deamination reaction Methods 0.000 claims abstract description 5
- 239000010802 sludge Substances 0.000 claims description 42
- 238000011084 recovery Methods 0.000 claims description 35
- 238000005406 washing Methods 0.000 claims description 25
- 239000007789 gas Substances 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 12
- 238000005086 pumping Methods 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims description 8
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- 238000004891 communication Methods 0.000 claims description 5
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- 238000001816 cooling Methods 0.000 claims description 2
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- 238000004821 distillation Methods 0.000 abstract description 7
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- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
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- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- 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
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Abstract
The invention discloses a coking wastewater and domestic sewage combined treatment system and a treatment method thereof, wherein the system comprises a collecting tank, a reaction sedimentation tank, an intermediate water tank, a pipeline mixer, a negative pressure steam stripping ammonia still, a comprehensive adjusting tank, a coagulating sedimentation tank, a pH adjusting tank, an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank which are sequentially communicated; the secondary sedimentation tank is also communicated with the anoxic tank; the coking wastewater is discharged into a collecting tank through a pipeline, and the domestic sewage is filtered by a grid and then is introduced into a comprehensive adjusting tank. The negative pressure stripping ammonia distillation tower deamination + A/A/O + precipitation treatment system designed by the invention can synchronously treat coking wastewater and domestic sewage, can recycle ammonia water, and can enable the sewage of coal chemical enterprises to reach the primary discharge standard of Integrated wastewater discharge Standard (GB 8978-1996).
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a coking wastewater and domestic sewage combined treatment system and a treatment method.
Background
The coking wastewater is generated in the processes of high-temperature dry distillation, gas purification and chemical product refining of raw coal, and comprises indirect cooling water, gas condensate water, gas desulfurization waste liquid, acid-base wastewater of a soft water station, boiler blow-off water, boiler cleaning wastewater and other wastewater, wherein main pollution factors are suspended matters, organic matters and ammonia nitrogen. Since 1/2009, the "admission conditions for the industry of the coking industry" requires that the phenol-cyanogen wastewater treatment shall implement the "Integrated wastewater discharge Standard" (GB8978-1996), and the discharge into the environment reaches the first-class standard. The standard requires that CODcr is less than or equal to 100mg/L and ammonia nitrogen is less than or equal to 15 mg/L.
At present, the mode of combining chemical separation and biochemical treatment is generally adopted at home and abroad to treat the wastewater. The chemical separation comprises unit processes such as steam stripping, extraction, rectification and the like to remove acid gas, recover phenol, ammonia and the like, and then carry out biochemical treatment, but a plurality of methods are often needed to be combined for use, the operation cost is high, and the emission requirement is difficult to achieve. Therefore, the treatment of the coking wastewater is always a great problem in the field of domestic and foreign wastewater treatment.
In addition, two independent treatment systems are mostly adopted by coking enterprises when coking wastewater and domestic sewage are treated, so that the problems of large floor area, high equipment investment, high operation cost and the like are caused.
Therefore, how to provide a coking wastewater and domestic sewage combined treatment system which has a simple process and can reach the discharge standard is a technical problem which needs to be solved urgently by the technical personnel in the field.
Disclosure of Invention
In view of the above, the invention provides a combined treatment system for coking wastewater and domestic sewage and a sewage treatment method using the system. The process is simple, the coking wastewater and the domestic sewage can be treated simultaneously, and the discharge requirements of national standards can be met.
In order to achieve the purpose, the invention adopts the following technical scheme:
a combined treatment system for coking wastewater and domestic sewage comprises a collecting tank, a reaction sedimentation tank, an intermediate water tank, a pipeline mixer, a negative pressure steam stripping ammonia still, a comprehensive adjusting tank, a coagulating sedimentation tank, a pH adjusting tank, an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank which are sequentially communicated; the secondary sedimentation tank is also communicated with the anoxic tank;
the coking wastewater is discharged into a collecting tank through a pipeline, and the domestic sewage is filtered by a grid and then is introduced into a comprehensive adjusting tank.
The main pollutants of the coking wastewater are COD and NH3N, SS, and the main pollutants to be treated are ammonia nitrogen, suspended matters and organic pollutants.
In order to reduce energy consumption, the ammonia distillation system adopts a negative pressure vacuum system, coking wastewater enters a negative pressure steam stripping ammonia distillation tower from the tower top, volatile free ammonia enters a gas phase under steam stripping because the relative volatility of ammonia is greater than that of water, new gas-liquid balance is established with liquid flowing down from a tower plate on the upper layer, after multiple times of gas-liquid phase balance, the ammonia concentration in the gas phase is improved to the design requirement, and ammonia steam is discharged from the tower top.
In the anaerobic tank, pollutants in the wastewater are hydrolyzed, acidified, broken and digested under the action of anaerobic bacteria and facultative bacteria. In the aerobic process section, organic pollutants are fully digested into water, carbon dioxide, cells, life energy, other inorganic matters and the like under the metabolism of aerobic bacteria; the ammonia nitrogen substances are converted into nitrite nitrogen or nitrate nitrogen by nitrifying bacteria through aerobic biochemical treatment to be removed. And the sludge in the secondary sedimentation tank flows back to the anoxic tank to supplement denitrifying bacteria, and the residual sludge is discharged to the sludge tank.
Further, the treatment system also comprises a sludge tank, and the reaction sedimentation tank, the coagulation sedimentation tank and the secondary sedimentation tank are communicated with the sludge tank.
Further, the treatment system also comprises a pneumatic diaphragm pump and a diaphragm filter press, and the sludge tank is communicated with the pneumatic diaphragm pump and the diaphragm filter press in sequence.
Further, still include ammonia recovery system and wash ammonia clarifier in above-mentioned processing system, negative pressure steam stripping ammonia still with ammonia recovery system intercommunication, collecting pit, middle pond, ammonia recovery system all with wash ammonia clarifier intercommunication.
Further, in the treatment system, the ammonia recovery system comprises a condenser, a vapor-liquid separation tank, a cooler, an ammonia pumping mixer, an ammonia recovery device, a reflux pump, a circulating pump and an ammonia pump;
the negative pressure steam stripping ammonia still is communicated with the condenser, the ammonia extraction mixer, the ammonia recovery device and the ammonia pump in sequence;
the condenser is communicated with the negative pressure steam stripping ammonia still through the steam-liquid separation tank and the reflux pump in sequence;
the circulating pump and the cooler are sequentially connected between the ammonia recovery device and the ammonia extraction mixer;
the ammonia recovery unit is in communication with the ammonia scrubber.
Further, the treatment system also comprises a lifting pump, a heat exchanger, a water outlet pump and a second pH adjusting tank;
the pipeline mixer is communicated with the top of the negative pressure steam stripping ammonia still through the lift pump and the heat exchanger in sequence;
the bottom of the negative pressure stripping ammonia still is communicated with the heat exchanger through the water outlet pump;
and the heat exchanger is communicated with the comprehensive adjusting tank through the second pH adjusting-back tank.
A combined treatment method of coking wastewater and domestic sewage adopts the treatment system, and comprises the following steps:
(1) after the coking wastewater enters a collecting tank, volatilizing part of ammonia gas in the coking wastewater to enter an ammonia washing purifier, and pumping the rest coking wastewater into a reaction sedimentation tank; adding a flocculating agent into the reaction sedimentation tank to precipitate suspended matters in the coking wastewater to form sludge, and discharging the sludge into a sludge tank;
(2) the coking wastewater in the reaction sedimentation tank enters an intermediate water tank, part of ammonia gas is volatilized again, and the volatilized ammonia gas enters an ammonia washing purifier; the coking wastewater in the intermediate water tank is mixed with alkali through a pipeline mixer and enters the top of a negative pressure steam stripping ammonia still;
(3) introducing steam into the bottom of the negative pressure steam stripping ammonia still, and discharging ammonia in the coking wastewater from the top of the tower to enter an ammonia recovery system to generate ammonia water through steam stripping; the wastewater at the bottom of the negative pressure steam stripping ammonia still enters a comprehensive regulating tank to be mixed with domestic sewage to form mixed sewage;
(4) the mixed sewage enters a coagulating sedimentation tank for coagulating sedimentation, and the generated sludge enters a sludge tank;
(5) the effluent of the coagulating sedimentation tank enters an anaerobic tank, an anoxic tank and an aerobic tank in turn for biochemical treatment after the pH of the effluent is adjusted by acid in a pH adjusting tank; the effluent of the aerobic tank enters a secondary sedimentation tank for further sedimentation and then is discharged after reaching the standard; one part of sludge in the secondary sedimentation tank flows back to the anoxic tank, and the other part of sludge is discharged into the sludge tank;
(6) sludge in the sludge pool enters a membrane filter press through a pneumatic membrane pump for filter pressing, and filter cakes obtained after filter pressing are subjected to environment-friendly and safe treatment; the ammonia gas in the ammonia washing purifier is washed and then is discharged in a high-emission standard.
Further, in the coking wastewater and domestic sewage combined treatment method, coking wastewater in a pipeline mixer is pumped into a heat exchanger through a lifting pump for preheating, then enters the top of a negative pressure stripping deamination tower, ammonia steam extracted by a negative pressure stripping ammonia still overflows from the top of the tower and enters a condenser, ammonia-containing condensate water flows back into the tower through a steam-liquid separation tank and a reflux pump, wastewater at the bottom of the tower enters a second pH regulation tank for regulating pH after heat exchange through the heat exchanger, then enters a comprehensive regulation tank, ammonia gas in the ammonia-containing condensate water is pumped into an ammonia recovery device through an ammonia pumping mixer, ammonia water at the bottom of the ammonia recovery device enters a cooler through a circulating pump for cooling and then enters an ammonia pumping mixer for refluxing, and concentrated ammonia water generated after recycling is pumped out by an ammonia pump for recycling; the recovered tail gas enters an ammonia washing purifier, ammonia in the recovered tail gas is removed through water washing to generate ammonia water with a certain concentration, the purified gas after water washing is discharged at high altitude, and the water inlet amount of the ammonia washing purifier is controlled to reach the required ammonia water concentration; the ammonia nitrogen of the wastewater at the bottom of the negative pressure steam stripping ammonia still is less than or equal to 30 mg/L.
Further, in the coking wastewater and domestic sewage combined treatment method, the pipeline mixer supplements alkali through the alkali adding device until the pH value of the coking wastewater is more than or equal to 10.5.
Further, in the coking wastewater and domestic sewage combined treatment method, the mass concentration of concentrated ammonia water generated after the ammonia recovery device is recycled is 15-18%, and ammonia-containing gas in the ammonia washing purifier is washed into 10-15% ammonia water by water spraying and can be reused as a fly ash boiler flue gas SNCR denitration agent.
According to the technical scheme, compared with the prior art, the invention discloses and provides a combined treatment system for coking wastewater and domestic sewage and a method for treating sewage by adopting the system. The negative pressure stripping ammonia distillation tower deamination + A/A/O (anaerobic-anoxic-aerobic) + precipitation treatment system designed by the invention can synchronously treat coking wastewater and domestic sewage, can recycle ammonia water, and can enable the sewage of coal chemical enterprises to reach the first-level discharge standard of Integrated wastewater discharge Standard (GB8978-1996) by adopting the treatment system.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a general process flow diagram of a coking wastewater and domestic sewage combined treatment system of the invention;
FIG. 2 is a process flow diagram of the negative pressure stripping ammonia distillation and ammonia recovery system of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. 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.
A combined treatment system for coking wastewater and domestic sewage comprises a collecting tank, a reaction sedimentation tank, an intermediate water tank, a pipeline mixer, a negative pressure steam stripping ammonia still, a comprehensive adjusting tank, a coagulating sedimentation tank, a pH adjusting tank, an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank which are sequentially communicated; the secondary sedimentation tank is also communicated with the anoxic tank;
coking wastewater is discharged into a collecting tank through a pipeline, and domestic sewage is filtered by a grid and then is introduced into a comprehensive adjusting tank.
In order to further optimize the technical scheme, the system also comprises a sludge tank, and the reaction sedimentation tank, the coagulating sedimentation tank and the secondary sedimentation tank are communicated with the sludge tank.
In order to further optimize the technical scheme, the device further comprises a pneumatic diaphragm pump and a diaphragm filter press, and the sludge tank is communicated with the pneumatic diaphragm pump and the diaphragm filter press in sequence.
In order to further optimize the technical scheme, the device also comprises an ammonia recovery system and an ammonia washing purifier, wherein the negative pressure stripping ammonia distillation tower is communicated with the ammonia recovery system, and the collecting tank, the intermediate water tank and the ammonia recovery system are communicated with the ammonia washing purifier.
In order to further optimize the technical scheme, the ammonia recovery system comprises a condenser, a vapor-liquid separation tank, a cooler, an ammonia pumping mixer, an ammonia recovery device, a reflux pump, a circulating pump and an ammonia pump;
the negative pressure steam stripping ammonia still is communicated with a condenser, an ammonia extraction mixer, an ammonia recovery device and an ammonia pump in sequence;
the condenser is communicated with the negative pressure steam stripping ammonia still through a steam-liquid separation tank and a reflux pump in sequence;
a circulating pump and a cooler are sequentially connected between the ammonia recovery device and the ammonia extraction mixer;
the ammonia recovery device is communicated with the ammonia washing purifier.
In order to further optimize the technical scheme, the system also comprises a lifting pump, a heat exchanger, a water outlet pump and a second pH adjusting tank;
the pipeline mixer is communicated with the top of the negative pressure steam stripping ammonia still through a lift pump and a heat exchanger in sequence;
the tower bottom of the negative pressure steam stripping ammonia still is communicated with the heat exchanger through a water outlet pump;
the heat exchanger is communicated with the comprehensive adjusting tank through a second pH adjusting-back tank.
Specifically, the method for performing combined treatment on the coking wastewater and the domestic sewage by adopting the treatment system comprises the following steps:
(1) after the coking wastewater enters a collecting tank, volatilizing part of ammonia gas in the coking wastewater to enter an ammonia washing purifier, and pumping the rest coking wastewater into a reaction sedimentation tank; adding a flocculating agent into the reaction sedimentation tank to precipitate suspended matters in the coking wastewater to form sludge, and discharging the sludge into a sludge tank;
(2) the coking wastewater in the reaction sedimentation tank enters an intermediate water tank, part of ammonia gas is volatilized again, and the volatilized ammonia gas enters an ammonia washing purifier; the coking wastewater in the intermediate water tank is mixed with alkali through a pipeline mixer and enters the top of a negative pressure steam stripping ammonia still;
(3) introducing steam into the bottom of the negative pressure steam stripping ammonia still, and discharging ammonia in the coking wastewater from the top of the tower to enter an ammonia recovery system to generate ammonia water through steam stripping; the wastewater at the bottom of the negative pressure steam stripping ammonia still enters a comprehensive regulating tank to be mixed with domestic sewage to form mixed sewage;
(4) the mixed sewage enters a coagulating sedimentation tank for coagulating sedimentation, and the generated sludge enters a sludge tank;
(5) the effluent of the coagulating sedimentation tank enters an anaerobic tank, an anoxic tank and an aerobic tank in turn for biochemical treatment after the pH of the effluent is adjusted by acid in a pH adjusting tank; the effluent of the aerobic tank enters a secondary sedimentation tank for further sedimentation and then is discharged after reaching the standard; one part of sludge in the secondary sedimentation tank flows back to the anoxic tank, and the other part of sludge is discharged into the sludge tank;
(6) sludge in the sludge pool enters a membrane filter press through a pneumatic membrane pump for filter pressing, and filter cakes obtained after filter pressing are subjected to environment-friendly and safe treatment; the ammonia gas in the ammonia washing purifier is washed and then is discharged in a high-emission standard.
In order to further optimize the technical scheme, coking wastewater in a pipeline mixer is pumped into a heat exchanger through a lifting pump to be preheated, then enters the top of a negative pressure stripping deamination tower, ammonia steam extracted by a negative pressure stripping ammonia still overflows from the top of the tower and enters a condenser, ammonia-containing condensate water flows back into the tower through a steam-liquid separation tank and a reflux pump, the wastewater at the bottom of the tower enters a second pH regulation tank to regulate the pH after heat exchange of the heat exchanger, then enters a comprehensive regulation tank, ammonia gas in the ammonia-containing condensate water is pumped into an ammonia recovery device through an ammonia pumping mixer, ammonia water at the bottom of the ammonia recovery device enters an ammonia pumping mixer to be refluxed after entering a cooler through a circulating pump, and concentrated ammonia water generated after recycling is pumped out and recycled through an ammonia pump; the recovered tail gas enters an ammonia washing purifier, ammonia in the recovered tail gas is removed through water washing to generate ammonia water with a certain concentration, the purified gas after water washing is discharged at high altitude, and the water inlet amount of the ammonia washing purifier is controlled to reach the required ammonia water concentration; the ammonia nitrogen of the wastewater at the bottom of the negative pressure steam stripping ammonia still is less than or equal to 30 mg/L.
The system is used for coking wastewater with 292m3And d, domestic sewage: 8-10m3And d, a certain coalification enterprise realizes the requirement of emission reaching the standard, and the process parameters and the equipment list are as follows.
1.1. Scale and characteristics
(1) Coking wastewater: 292m3D (ammonia-containing wastewater), contains suspended matters, ammonia nitrogen and organic matters, has lower B/C ratio and is not easy to generate biochemical reaction;
(2) domestic sewage: 8-10m3D, containing organic matters, suspended matters, ammonia nitrogen and a small amount of oil, and having high B/C ratio and easy biochemistry;
see table 1 below for specific parameters:
table 1: coking wastewater and domestic sewage parameters
1.2. Designed water quantity
According to the data provided by the owner, the water quantity of the production wastewater is about 292m3D, the water quantity of domestic sewage is about 8-10m3D, total water amount is 300m3And d. The scheme designs the treatment system to operate for 24 hours, and the treatment water amount is 12.5m3D, maximum daily water treatment amount is 300m3And d. The concentration of the ammonia nitrogen in the inlet water treated by the negative pressure ammonia distillation system is 1000mg/l, and can reach 1200mg/l at most.
1.3. Effluent discharge execution standard
The wastewater of the project reaches the first-class discharge standard of Integrated wastewater discharge Standard (GB8978-1996) after being treated by a treatment system. The specific effluent quality index parameters are shown in the following table 2.
TABLE 2 Water quality index Limit (unit: mg/L, except PH)
1.4. Sewage treatment system equipment inventory
TABLE 3 Sewage treatment System Equipment List
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (8)
1. A combined treatment system for coking wastewater and domestic sewage is characterized by comprising a collecting tank, a reaction sedimentation tank, an intermediate water tank, a pipeline mixer, a negative pressure steam stripping ammonia still, a comprehensive adjusting tank, a coagulating sedimentation tank, a pH adjusting tank, an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank which are sequentially communicated; the secondary sedimentation tank is also communicated with the anoxic tank;
the coking wastewater is discharged into a collecting tank through a pipeline, and the domestic sewage is filtered by a grid and then is introduced into a comprehensive adjusting tank.
2. The treatment system of claim 1, further comprising a sludge tank, wherein the reaction sedimentation tank, the coagulation sedimentation tank and the secondary sedimentation tank are all communicated with the sludge tank.
3. The treatment system of claim 2, further comprising a pneumatic diaphragm pump and a diaphragm filter press, wherein the sludge pond is in communication with the pneumatic diaphragm pump and the diaphragm filter press in sequence.
4. The treatment system of claim 3, further comprising an ammonia recovery system and an ammonia scrubber, wherein the negative pressure stripping ammonia still is in communication with the ammonia recovery system, and wherein the collection sump, the intermediate water sump, and the ammonia recovery system are in communication with the ammonia scrubber.
5. The treatment system of claim 4, wherein the ammonia recovery system comprises a condenser, a vapor-liquid separation tank, a cooler, an ammonia extraction mixer, an ammonia recovery device, a reflux pump, a circulation pump, an ammonia pump;
the negative pressure steam stripping ammonia still is communicated with the condenser, the ammonia extraction mixer, the ammonia recovery device and the ammonia pump in sequence;
the condenser is communicated with the negative pressure steam stripping ammonia still through the steam-liquid separation tank and the reflux pump in sequence;
the ammonia recovery device is connected with the ammonia extraction mixer sequentially through the circulating pump and the cooler;
the ammonia recovery unit is in communication with the ammonia scrubber.
6. The treatment system of claim 5, further comprising a lift pump, a heat exchanger, a water outlet pump, a second pH adjustment tank;
the pipeline mixer is communicated with the top of the negative pressure steam stripping ammonia still through the lift pump and the heat exchanger in sequence;
the bottom of the negative pressure stripping ammonia still is communicated with the heat exchanger through the water outlet pump;
and the heat exchanger is communicated with the comprehensive adjusting tank through the second pH adjusting-back tank.
7. A combined treatment method of coking wastewater and domestic sewage, which is characterized in that the treatment system of claim 6 is adopted, and comprises the following steps:
(1) after the coking wastewater enters a collecting tank, volatilizing part of ammonia gas in the coking wastewater to enter an ammonia washing purifier, and pumping the rest coking wastewater into a reaction sedimentation tank; adding a flocculating agent into the reaction sedimentation tank to precipitate suspended matters in the coking wastewater to form sludge, and discharging the sludge into a sludge tank;
(2) the coking wastewater in the reaction sedimentation tank enters an intermediate water tank, part of ammonia gas is volatilized again, and the volatilized ammonia gas enters an ammonia washing purifier; the coking wastewater in the intermediate water tank is mixed with alkali through a pipeline mixer and enters the top of a negative pressure steam stripping ammonia still;
(3) introducing steam into the bottom of the negative pressure steam stripping ammonia still, and discharging ammonia in the coking wastewater from the top of the tower to enter an ammonia recovery system to generate ammonia water through steam stripping; the wastewater at the bottom of the negative pressure steam stripping ammonia still enters a comprehensive regulating tank to be mixed with domestic sewage to form mixed sewage;
(4) the mixed sewage enters a coagulating sedimentation tank for coagulating sedimentation, and the generated sludge enters a sludge tank;
(5) the effluent of the coagulating sedimentation tank enters an anaerobic tank, an anoxic tank and an aerobic tank in turn for biochemical treatment after the pH of the effluent is adjusted by acid in a pH adjusting tank; the effluent of the aerobic tank enters a secondary sedimentation tank for further sedimentation and then is discharged after reaching the standard; one part of sludge in the secondary sedimentation tank flows back to the anoxic tank, and the other part of sludge is discharged into the sludge tank;
(6) sludge in the sludge pool enters a membrane filter press through a pneumatic membrane pump for filter pressing, and filter cakes obtained after filter pressing are subjected to environment-friendly and safe treatment; the ammonia gas in the ammonia washing purifier is washed and then is discharged in a high-emission standard.
8. The coking wastewater and domestic sewage combined treatment method according to claim 7, characterized in that the coking wastewater in the pipeline mixer is pumped into a heat exchanger through a lift pump for preheating, then enters the top of a negative pressure stripping deamination tower, ammonia steam extracted by a negative pressure stripping ammonia still overflows from the top of the tower and enters a condenser, ammonia-containing condensate water flows back into the tower through a vapor-liquid separation tank and a reflux pump, the wastewater at the bottom of the tower enters a second pH adjustment tank for pH adjustment after heat exchange through the heat exchanger, then enters a comprehensive adjustment tank, ammonia gas in the ammonia-containing condensate water is pumped into an ammonia recovery device through an ammonia pumping mixer, ammonia water at the bottom of the ammonia recovery device enters a cooler through a circulating pump for cooling and then enters an ammonia pumping mixer for reflux, and concentrated ammonia water generated after recycling is pumped out through an ammonia pump for recycling; the recovered tail gas enters an ammonia washing purifier, ammonia in the recovered tail gas is removed through water washing to generate ammonia water with a certain concentration, the purified gas after water washing is discharged at high altitude, and the water inlet amount of the ammonia washing purifier is controlled to reach the required ammonia water concentration; the ammonia nitrogen of the wastewater at the bottom of the negative pressure steam stripping ammonia still is less than or equal to 30 mg/L.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880112A (en) * | 2010-07-06 | 2010-11-10 | 武汉钢铁(集团)公司 | Coking wastewater treatment process |
| CN104591458A (en) * | 2014-02-21 | 2015-05-06 | 江苏夏航环境工程有限公司 | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process |
| CN108558134A (en) * | 2018-04-11 | 2018-09-21 | 宝钢工程技术集团有限公司 | A kind of processing system of coking wastewater removing total nitrogen |
| CN112723663A (en) * | 2020-12-16 | 2021-04-30 | 河南利源燃气有限公司 | Novel coking full-water system water treatment process |
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2021
- 2021-09-25 CN CN202111124945.0A patent/CN113772892A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880112A (en) * | 2010-07-06 | 2010-11-10 | 武汉钢铁(集团)公司 | Coking wastewater treatment process |
| CN104591458A (en) * | 2014-02-21 | 2015-05-06 | 江苏夏航环境工程有限公司 | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process |
| CN108558134A (en) * | 2018-04-11 | 2018-09-21 | 宝钢工程技术集团有限公司 | A kind of processing system of coking wastewater removing total nitrogen |
| CN112723663A (en) * | 2020-12-16 | 2021-04-30 | 河南利源燃气有限公司 | Novel coking full-water system water treatment process |
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