CN111072146A - Treatment system and treatment method for high-COD high-ammonia nitrogen wastewater - Google Patents
Treatment system and treatment method for high-COD high-ammonia nitrogen wastewater Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 101
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 189
- 238000006396 nitration reaction Methods 0.000 claims abstract description 21
- 238000005273 aeration Methods 0.000 claims abstract description 8
- 239000010802 sludge Substances 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 15
- 230000001105 regulatory effect Effects 0.000 claims description 14
- 238000012806 monitoring device Methods 0.000 claims description 8
- 206010021143 Hypoxia Diseases 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 2
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- 230000001276 controlling effect Effects 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000003513 alkali Substances 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 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 7
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- 229910052799 carbon Inorganic materials 0.000 description 7
- 238000012544 monitoring process Methods 0.000 description 7
- 230000001546 nitrifying effect Effects 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 229910052698 phosphorus Inorganic materials 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
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- 229910002651 NO3 Inorganic materials 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 244000052616 bacterial pathogen Species 0.000 description 1
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- 210000003608 fece Anatomy 0.000 description 1
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- 239000010871 livestock manure Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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- 238000006386 neutralization reaction Methods 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 150000002826 nitrites Chemical class 0.000 description 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous oxide Inorganic materials [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 150000007530 organic bases Chemical class 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
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- 238000003672 processing method Methods 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
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- 239000004065 semiconductor Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to the technical field of wastewater treatment, in particular to a treatment system and a treatment method for high-COD high-ammonia nitrogen wastewater. The treatment system comprises an anaerobic reaction tank, an anoxic reaction tank, a first aerobic reaction tank, a second aerobic reaction tank and a third aerobic reaction tank which are sequentially connected, and aeration devices respectively connected with the anaerobic reaction tank, the anoxic reaction tank, the first aerobic reaction tank, the second aerobic reaction tank and the third aerobic reaction tank. According to the treatment system and the treatment method for the high-COD high-ammonia-nitrogen wastewater, disclosed by the invention, the anaerobic reaction, the anoxic denitrification reaction, the aerobic reaction and the two-stage nitration reaction are sequentially carried out on the wastewater, and by adopting the mode, the COD concentration in the wastewater is firstly reduced, then the two-stage nitration reaction is carried out, so that the inhibition of the high-COD concentration on the nitration reaction is avoided, and the wastewater treatment effect is good.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the technical field of wastewater treatment, in particular to a treatment system and a treatment method for high-COD high-ammonia nitrogen wastewater.
[ background of the invention ]
The treatment method in the prior art is to treat high-COD high-ammonia nitrogen wastewater by a method of arranging an adjusting tank, an anaerobic tank, an anoxic tank, an aerobic tank and a sedimentation tank, and the method has the following defects: first, theFirstly, the process for treating the high-COD high-ammonia nitrogen wastewater is unstable, cannot resist impact load, is difficult to operate and control, and is difficult to achieve the treatment purpose; secondly, the COD concentration in the wastewater is high, which can inhibit the nitration reaction of the system to a certain extent, and the realization of the NH reaction of the system is difficult4 +-a deep removal of N; thirdly, the method belongs to the traditional activated sludge method, the independence of the activated sludge can not be realized, and the activity of the sludge is easily influenced by the fluctuation of the quality of the inlet water.
[ summary of the invention ]
The invention aims to provide a treatment system and a treatment method for high-COD high-ammonia nitrogen wastewater, which aim to solve the problems in the prior art.
The invention provides a treatment system for high-COD high-ammonia nitrogen wastewater, which comprises an anaerobic reaction tank, an anoxic reaction tank, a first aerobic reaction tank, a second aerobic reaction tank and a third aerobic reaction tank which are connected in sequence, and aeration devices respectively connected with the anaerobic reaction tank, the anoxic reaction tank, the first aerobic reaction tank, the second aerobic reaction tank and the third aerobic reaction tank.
Preferably, the processing system still include with the equalizing basin that the anaerobic reaction pond is connected, respectively with the anaerobic reaction pond the oxygen deficiency reaction pond first aerobic reaction pond with the mud collecting tank that the aerobic reaction pond of second is connected, with the play water buffer pool that the aerobic reaction pond of third is connected and respectively with the anaerobic reaction pond the oxygen deficiency reaction pond first aerobic reaction pond second aerobic reaction pond with the on-line monitoring device that the aerobic reaction pond of third is connected, on-line monitoring device is used for monitoring pH value, redox potential and sludge concentration in each reaction pond.
Preferably, the treatment system further comprises an alkali liquor storage device respectively connected with the second aerobic reaction tank and the third aerobic reaction tank, the third aerobic reaction tank is connected with the anoxic reaction tank through a reflux device, and the regulating tank is connected with the anaerobic reaction tank through a water inlet device.
The invention also provides a treatment method of the high COD high ammonia nitrogen wastewater, which utilizes the treatment system to treat the wastewater, and the treatment method comprises the following steps:
introducing the wastewater into the anaerobic reaction tank to perform anaerobic reaction;
introducing the wastewater into the anoxic reaction tank for denitrification reaction;
introducing the wastewater into the first aerobic reaction tank for aerobic reaction;
introducing the wastewater into the second aerobic reaction tank to perform a first-stage nitration reaction;
and introducing the wastewater into the third aerobic reaction tank to perform a second-stage nitration reaction.
Preferably, the treatment method further comprises, before the anaerobic reaction:
and introducing the wastewater into the regulating tank, and regulating the pH value of the wastewater to 7.5-8.5.
Preferably, in the anaerobic reaction process of the wastewater, the DO value is controlled to be 0.12 mg/L-0.18 mg/L, and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L.
Preferably, in the process of the denitrification reaction of the wastewater, the DO value is controlled to be 0.30 mg/L-0.80 mg/L, and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L.
Preferably, in the aerobic reaction process of the wastewater, the DO value is controlled to be 4.07 mg/L-5.23 mg/L, and the sludge concentration is controlled to be 5300 mg/L-5700 mg/L.
Preferably, in the first-stage nitration reaction process of the wastewater, the DO value is controlled to be 4.23 mg/L-5.67 mg/L, the sludge concentration is controlled to be 5300 mg/L-5700 mg/L, and the pH value is controlled to be more than or equal to 7.0.
Preferably, the DO value is controlled to be 4.66 mg/L-5.78 mg/L and the pH value is controlled to be more than or equal to 7.0 during the secondary nitration reaction of the wastewater.
The invention has the beneficial effects that: according to the treatment system and the treatment method for the high-COD high-ammonia-nitrogen wastewater, disclosed by the invention, the anaerobic reaction, the anoxic denitrification reaction, the aerobic reaction and the two-stage nitration reaction are sequentially carried out on the wastewater, and by adopting the mode, the COD concentration in the wastewater is firstly reduced, then the two-stage nitration reaction is carried out, so that the inhibition of the high-COD concentration on the nitration reaction is avoided, and the wastewater treatment effect is good.
[ description of the drawings ]
FIG. 1 is a schematic structural diagram of a high COD high ammonia nitrogen wastewater treatment system provided in embodiment 1 of the present invention;
FIG. 2 is a flow chart of a method for treating high COD and high ammonia nitrogen wastewater provided by embodiment 2 of the present invention.
[ detailed description ] embodiments
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 only a part of the embodiments of the present invention, and not all of the 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.
The terms "first", "second" and "third" in the present invention are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," or "third" may explicitly or implicitly include at least one of the feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise. All directional indicators (such as up, down, left, right, front, and rear … …) in the embodiments of the present invention are only used to explain the relative positional relationship between the components, the movement, and the like in a specific posture (as shown in the drawings), and if the specific posture is changed, the directional indicator is changed accordingly. Furthermore, the terms "include" and "have," as well as any variations thereof, are intended to cover non-exclusive inclusions.
Reference herein to "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment can be included in at least one embodiment of the invention. The appearances of the phrase in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments. It is explicitly and implicitly understood by one skilled in the art that the embodiments described herein can be combined with other embodiments.
In this specification, COD is Chemical Oxygen Demand (Chemical Oxygen Demand) and is a method for chemically measuring the amount of reducing substances to be oxidized in a water sample; DO is dissolved oxygen (dissolved oxygen), which is molecular oxygen in air dissolved in water; the ammonia nitrogen is NH4 +N in the form of NO3 -Form of N, nitrous nitrogen as NO2 -Form N.
Nitrifying bacteria (Nitrifying bacteria) are an aerobic bacteria, including nitrites and nitrates. Living in aerobic water or sand bed, plays an important role in the water purification process of nitrogen circulation. The nitrifying bacteria are widely found in all corners of nature, air, rivers, sea and soil, and thousands of nitrifying bacteria are found in biology. Denitrifying bacteria are bacteria that cause denitrification. Heterotrophic, facultative anaerobic bacteria such as denitrifying bacilli, Sterlla, Fluoropolar Aerobacter, and the like are most common. Under the condition of xenon, the oxygen in nitric acid is utilized to oxidize organic substances so as to obtain the energy required by the life activity of the organic substances. Denitrifying bacteria are widely distributed in soil, manure and sewage. Nitrate nitrogen can be converted into nitrogen instead of ammonia, which is not completely opposite to the effect of nitrifying bacteria. The method is mainly applied to sewage treatment. Nitrification and denitrification composite strain: the composite strain with double functions of nitrification and denitrification can propagate automatically according to the water quality condition, so that the strain balance is achieved, and the sewage treatment work is simpler and more efficient.
Example 1
The embodiment 1 of the invention provides a treatment system for high-COD high-ammonia nitrogen wastewater, and please refer to fig. 1, the treatment system comprises an adjusting tank 10, an anaerobic reaction tank 20, an anoxic reaction tank 30, a first aerobic reaction tank 40, a second aerobic reaction tank 50, a third aerobic reaction tank 60 and an effluent buffer tank 70 which are connected in sequence, the pH value of the wastewater is adjusted to a required value in the adjusting tank 10 and then introduced into the anaerobic reaction tank 20 for reaction, a water inlet device 101 is further arranged between the adjusting tank 10 and the anaerobic reaction tank 20, and the water inlet device 101 can be a water inlet pump. In this embodiment, the third aerobic reaction tank 60 is connected to the anoxic reaction tank 30 through a backflow device 601 to backflow the wastewater in the third aerobic reaction tank 60 to the anoxic reaction tank 30, the backflow device 601 may be a backflow pump, and the treated wastewater flows out of the third aerobic reaction tank 60 into the effluent buffer tank 70.
In this embodiment, the treatment system is further provided with an aeration device 80, and the aeration device 80 is connected with the anaerobic reaction tank 20, the anoxic reaction tank 30, the first aerobic reaction tank 40, the second aerobic reaction tank 50 and the third aerobic reaction tank 60, and is used for aerating the reaction tanks to adjust the OD value in the reaction tanks. The aeration device 80 may be a blower.
In this embodiment, the treatment system is further provided with an online monitoring device (not shown), which is respectively connected with the anaerobic reaction tank 20, the anoxic reaction tank 30, the first aerobic reaction tank 40, the second aerobic reaction tank 50 and the third aerobic reaction tank 60, and is used for monitoring the pH value, the oxidation-reduction potential and the sludge concentration in each reaction tank. In an alternative embodiment, the on-line monitoring device further comprises a pH monitor, an OPR on-line monitor for monitoring redox capacity, and a MLSS on-line monitor for monitoring sludge concentration.
In an alternative embodiment, when the COD concentration of the wastewater in the regulating tank 10 is more than 4000mg/L or ammonia Nitrogen (NH)4 +and-N) when the concentration is more than 300mg/L, automatically starting the sewage lifting pump, switching to the accident pool for temporary storage, then conveying a small amount of sewage from the accident pool to the regulating pool 10, and treating the sewage after the regulated sewage reaches the water quality standard of the inlet water. That is, in order to improve the wastewater treatment effect, it is necessary to control the COD concentration in the wastewater entering the anaerobic reaction tank 20 to 4000mg/L or less and the ammonia Nitrogen (NH) in the wastewater4 +-N) at a concentration of less than or equal to 300 mg/L.
In an optional embodiment, the treatment system is further provided with a sludge collecting tank 901, a sludge screw pump 902 and a belt filter press 903 which are connected with the sludge collecting tank 901, the anaerobic reaction tank 20, the anoxic reaction tank 30, the first aerobic reaction tank 40 and the second aerobic reaction tank 50 are respectively provided with a sludge discharge valve at the bottom thereof, the sludge collecting tank 901 is respectively connected with the anaerobic reaction tank 20, the anoxic reaction tank 30, the first aerobic reaction tank 40 and the second aerobic reaction tank 50 through different sludge discharge valves, when the on-line monitoring device monitors that the sludge concentration of any one of the anaerobic reaction tank 20, the anoxic reaction tank 30, the first aerobic reaction tank 40 and the second aerobic reaction tank 50 is more than or equal to 6000mg/L, the operation of a sludge discharge valve of the corresponding reaction tank is controlled, so as to discharge the sludge in the corresponding reaction tank into the sludge collecting tank 901 until the sludge concentration in the corresponding reaction tank is less than 6000 mg/L. The sludge in the sludge collection tank 901 is introduced into a belt filter press 903 through a sludge screw pump 902, the belt filter press 903 dehydrates the sludge, the obtained filter cake is transported to a landfill, and the obtained press filtration water is returned to the adjusting tank 10 to be used as wastewater for retreatment.
In an optional embodiment, the treatment system is further provided with an alkali liquor storage device 904, the alkali liquor storage device 904 is respectively connected with the second aerobic reaction tank 50 and the third aerobic reaction tank 60, when the online monitoring device monitors that the pH value in the second aerobic reaction tank 50 or the third aerobic reaction tank 60 is less than or equal to 7.0, the alkali liquor is conveyed from the alkali liquor storage device 904 to the second aerobic reaction tank 50 or the third aerobic reaction tank 60, so as to adjust the pH value in the second aerobic reaction tank 50 or the third aerobic reaction tank 60 to be greater than 7.0.
In an alternative embodiment, the anaerobic reaction tank 20 is constructed with a biological fluidized bed, the anoxic reaction tank 30 is constructed with a biological fluidized bed, the first aerobic reaction tank 40 is constructed with a biological fluidized bed, the second aerobic reaction tank 50 is constructed with a biological fluidized bed, and the third aerobic reaction tank 60 is constructed with an aerated biological filter.
In an optional embodiment, the pH value of the wastewater in the regulating tank 10 is controlled to be 7.5-8.5; controlling the DO value of the wastewater in the anaerobic reaction tank 20 to be 0.12 mg/L-0.18 mg/L, and controlling the sludge concentration of the wastewater in the anaerobic reaction tank 20 to be 4800 mg/L-5200 mg/L; controlling the DO value of the wastewater in the anoxic reaction tank 30 to be 0.30-0.80 mg/L, and controlling the sludge concentration of the wastewater in the anoxic reaction tank 30 to be 4800-5200 mg/L; controlling the DO value of the wastewater in the first aerobic reaction tank 40 to be 4.07-5.23 mg/L, and controlling the sludge concentration of the wastewater in the first aerobic reaction tank 40 to be 5300-5700 mg/L; controlling the DO value of the wastewater in the second aerobic reaction tank 50 to be 4.23 mg/L-5.67 mg/L, controlling the sludge concentration of the wastewater in the second aerobic reaction tank 50 to be 5300 mg/L-5700 mg/L, and controlling the pH value to be more than or equal to 7.0; controlling the DO value of the wastewater in the third aerobic reaction tank 60 to be 4.66 mg/L-5.78 mg/L, and controlling the pH value of the wastewater in the third aerobic reaction tank 60 to be more than or equal to 7.0.
Example 2
The embodiment 2 of the invention provides a method for treating high-COD high-ammonia nitrogen wastewater, which utilizes the treatment system of the embodiment 1 to treat the wastewater, and please refer to fig. 2, wherein the treatment method comprises the following steps:
s201, introducing the wastewater into the adjusting tank, and adjusting the pH value of the wastewater to 7.5-8.5.
In step S201, the pH of the wastewater is adjusted to 7.5 to 8.5 by adding an inorganic acid or an inorganic base, and the added acid and base may be an organic acid and an organic base commonly used in acid-base neutralization in the art.
In an alternative embodiment, it is desirable to control the COD concentration in the wastewater entering the anaerobic reaction tank 20 to be less than or equal to 4000mg/L and the ammonia Nitrogen (NH) concentration in the wastewater4 +-N) at a concentration of less than or equal to 300 mg/L.
S202, introducing the wastewater into the anaerobic reaction tank for anaerobic reaction.
In step S202, the wastewater undergoes an anaerobic reaction, in the anaerobic reaction process, bacteria in the sludge hydrolyze phosphorus accumulation in cells under anaerobic conditions, and utilize the energy of the hydrolyzed phosphorus accumulation to synthesize a carbon source, and the carbon source is stored in the bacteria, and the bacteria decompose macromolecular organic matters in the wastewater in the process of synthesizing the carbon source, so as to reduce the COD concentration of the wastewater. Through the anaerobic reaction, the COD concentration in the wastewater is greatly reduced, which is beneficial to the growth of nitrobacteria in the sludge.
In an optional embodiment, during the anaerobic reaction of the wastewater, the DO value is controlled to be 0.12 mg/L-0.18 mg/L, and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L.
S203, introducing the wastewater into the anoxic reaction tank for denitrification reaction.
In step S203, the wastewater is subjected to anoxic denitrification reaction, during which bacteria in the sludge, such as denitrifying phosphorus accumulating bacteria, are subjected to anoxic denitrification using energy (carbon source) stored in the bacteria as an electron donor and nitrate Nitrogen (NO)3 -And N) is an electron acceptor to perform denitrification nitrogen and phosphorus removal, and nitrate nitrogen forms nitrogen through denitrification, and energy (carbon source) in the denitrifying phosphorus-accumulating bacteria is consumed in the process.
In an optional embodiment, the DO value is controlled to be 0.30 mg/L-0.80 mg/L and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L in the denitrification reaction process of the wastewater.
S204, introducing the wastewater into the first aerobic reaction tank for aerobic reaction.
In step S204, the wastewater undergoes an aerobic reaction, and in the aerobic reaction process, the bacteria in the sludge decompose the energy (carbon source) stored in the bacteria to provide energy for cell growth and propagation, using the energy (carbon source) stored in the bacteria as an electron donor and oxygen as a final electron acceptor, and at the same time, decompose the small molecular organic matters in the wastewater to further reduce the COD concentration of the wastewater. After the aerobic reaction, the COD concentration in the wastewater is further reduced.
In an optional embodiment, the DO value is controlled to be 4.07 mg/L-5.23 mg/L and the sludge concentration is controlled to be 5300 mg/L-5700 mg/L during the aerobic reaction process of the wastewater.
S205, introducing the wastewater into the second aerobic reaction tank to perform a first-stage nitration reaction.
S206, introducing the wastewater into the third aerobic reaction tank for a second-stage nitration reaction.
In the steps S205 and S206, through the above processes, the COD concentration in the wastewater is greatly reduced, which is beneficial to improving the effect of the subsequent two-stage nitrification reaction, in the first-stage nitrification reaction process, nitrifying bacteria in the sludge oxidize ammonia nitrogen in the wastewater into nitrate nitrogen and nitrite nitrogen, the ammonia nitrogen in the wastewater is largely oxidized, meanwhile, organic matters in the wastewater are further decomposed, and the COD concentration in the wastewater is further reduced; in the second-stage nitration reaction process, under the lower COD concentration, the nitrifying bacteria in the sludge oxidize the residual ammonia nitrogen in the wastewater into nitrate nitrogen and nitrite nitrogen, the ammonia nitrogen in the wastewater is continuously oxidized, meanwhile, the organic matters in the wastewater are further decomposed, and the COD concentration of the wastewater is further reduced.
In an optional embodiment, during the first-stage nitration reaction of the wastewater, the DO value is controlled to be 4.23 mg/L-5.67 mg/L, the sludge concentration is controlled to be 5300 mg/L-5700 mg/L, and the pH value is controlled to be greater than or equal to 7.0; in the process of the secondary nitration reaction of the wastewater, the DO value is controlled to be 4.66 mg/L-5.78 mg/L, and the pH value is controlled to be more than or equal to 7.0.
The main control points of the treatment method of the embodiment are raw water COD and NH4 +N, and control of pH and DO concentration in each cell unit: 1. when COD in the regulating tank is more than 4000mg/L, NH4 +When N is more than 300mg/L, automatically starting a sewage lifting pump, switching to an accident pool for temporary storage, then conveying a small amount of sewage from the accident pool to an adjusting pool, and treating the sewage after the sewage reaches the water quality standard of the inlet water after the sewage is adjusted; 2. adding alkali liquor, wherein the alkali liquor is required to be supplemented from an alkali tank when the numerical value of the pH online monitor is lower than 7.0 when the aerobic tank carries out nitration reaction due to the fact that the nitration reaction consumes the alkalinity; 3. the main pollutants of the treatment method of this example were COD and NH4 +N, the principle of removing COD by the system is that macromolecule organic matters in the wastewater are degraded into micromolecule organic matters based on anaerobic conditions, further removal is realized under aerobic conditions, and the denitrification reaction of an anoxic tank is combined, so that the removal rate of the system to COD is ensured, NH is removed4 +The principle of the-N is nitrification and denitrification, ammonia nitrogen is converted into nitrite nitrogen and nitrate nitrogen through nitrification reaction, and NH is treated by combining multi-stage aerobic conditions and an aeration biological filter4 +Deep removal of N, wherein the nitration reaction is carried out by nitrobacteria microorganisms, and DO in an aerobic environment is required to be more than or equal to 4.2 mg/L; the COD in the effluent is less than 200mg/L and NH is strictly controlled at the point 34 +N is less than 1.5mg/L, NH4 +The water quality of the-N effluent reaches the national surface water environmental quality standard GB 3838-2002。
1. The design parameters of the processing method are selected
Designing main water quality indexes of inlet water: COD is less than or equal to 4000mg/L, and NH4+ -N is less than or equal to 300 mg/L;
designing main effluent quality indexes: COD is less than or equal to 200mg/L, and NH4+ -N is less than or equal to 1.5 mg/L.
2. Determination of ensuring proper operation of process
On-line monitoring equipment for monitoring the regulating tank, the anaerobic tank, the anoxic tank, the aerobic tank and the effluent buffer tank at any time in each operation period, and strictly controlling on-line instruments of each process within a control range by manually analyzing main water quality index concentrations of inlet water and outlet water so as to ensure that the system stably operates and reaches the standard, particularly NH4 +The water quality of the-N effluent reaches the national environmental quality standard for surface water GB 3838-2002.
a. When COD in the regulating tank is more than 4000mg/L, NH4 +And when the-N is more than 300mg/L, automatically starting the sewage lifting pump, switching to the accident pool for temporary storage, then conveying a small amount of sewage from the accident pool to the regulating pool, and treating the sewage after the regulated sewage reaches the water quality standard of the inlet water.
b. When the aerobic tank is in the aeration reaction stage, alkali liquor needs to be supplemented to the aerobic tank when the pH value is less than 7.0 because the alkalinity is consumed in the nitrification reaction, so that the nitrification reaction is kept to be smoothly carried out.
c. The concentration of MLSS in each reaction unit is 4000-6000 mg/L, SV30 is 20-30%, SVI is 60-100, the temperature is 25-35 ℃, DO is not less than 4.0mg/L in an aerobic environment, and DO is 0.12-0.18 mg/L in an anaerobic and anoxic environment.
d. And the online monitoring instrument is calibrated at regular time, so that the normal operation of the whole process is ensured.
The treatment method is applied to a purification workshop of Shenzhen hazardous waste company (the quality of inlet and outlet water is shown in Table 1), the quality of outlet water is stable when the Shenzhen hazardous waste company continuously runs from 11 and 10 months in 2018 to 11 and 10 months in 2019, the COD (chemical oxygen demand) in the outlet water is lower than 200mg/L, and NH (ammonia) is higher than NH4 +N is less than 1.5mg/L, NH4 +The water quality of the-N effluent reaches the national surface water environmental quality standard GB 3838-2002; the removal rate of COD is about95％，NH4 +the-N removal rate was about 99.5%. In a word, the method for treating the high-COD high-ammonia nitrogen wastewater has good effluent effect and obtains certain economic benefit and social benefit.
TABLE 1 wastewater influent and effluent Water quality parameters
While the foregoing is directed to embodiments of the present invention, it will be understood by those skilled in the art that various changes may be made without departing from the spirit and scope of the invention.
Claims (10)
1. The utility model provides a processing system of high COD high ammonia nitrogen waste water, its characterized in that, processing system including the anaerobic reaction pond, oxygen deficiency reaction tank, first aerobic reaction pond, second aerobic reaction pond and the third aerobic reaction pond that connect gradually and respectively with the anaerobic reaction pond oxygen deficiency reaction tank first aerobic reaction pond second aerobic reaction pond with the aeration equipment that the third aerobic reaction pond is connected.
2. The treatment system according to claim 1, further comprising an adjusting tank connected to the anaerobic reaction tank, sludge collecting tanks respectively connected to the anaerobic reaction tank, the anoxic reaction tank, the first aerobic reaction tank and the second aerobic reaction tank, an effluent buffer tank connected to the third aerobic reaction tank, and on-line monitoring devices respectively connected to the anaerobic reaction tank, the anoxic reaction tank, the first aerobic reaction tank, the second aerobic reaction tank and the third aerobic reaction tank, the on-line monitoring devices being configured to monitor pH, redox potential and sludge concentration in each reaction tank.
3. The treatment system according to claim 2, further comprising a lye storage device connected to the second aerobic reaction tank and the third aerobic reaction tank, respectively, wherein the third aerobic reaction tank is connected to the anoxic reaction tank through a reflux device, and the adjustment tank is connected to the anaerobic reaction tank through a water inlet device.
4. A method for treating high-COD high-ammonia nitrogen wastewater by using the treatment system of any one of claims 1 to 3, which is characterized by comprising the following steps:
introducing the wastewater into the anaerobic reaction tank to perform anaerobic reaction;
introducing the wastewater into the anoxic reaction tank for denitrification reaction;
introducing the wastewater into the first aerobic reaction tank for aerobic reaction;
introducing the wastewater into the second aerobic reaction tank to perform a first-stage nitration reaction;
and introducing the wastewater into the third aerobic reaction tank to perform a second-stage nitration reaction.
5. The process of claim 4, further comprising, prior to the anaerobic reaction:
and introducing the wastewater into the regulating tank, and regulating the pH value of the wastewater to 7.5-8.5.
6. The treatment method according to claim 4, wherein the DO value is controlled to be 0.12 mg/L-0.18 mg/L and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L during the anaerobic reaction of wastewater.
7. The treatment method according to claim 4, wherein the DO value is controlled to be 0.30 mg/L-0.80 mg/L and the sludge concentration is controlled to be 4800 mg/L-5200 mg/L during the denitrification reaction of the wastewater.
8. The treatment method as claimed in claim 4, wherein the DO value is controlled to be 4.07 mg/L-5.23 mg/L and the sludge concentration is controlled to be 5300 mg/L-5700 mg/L during the aerobic reaction of the wastewater.
9. The treatment method according to claim 4, wherein during the first stage nitrification reaction of wastewater, the DO value is controlled to be 4.23 mg/L-5.67 mg/L, the sludge concentration is controlled to be 5300 mg/L-5700 mg/L, and the pH value is controlled to be greater than or equal to 7.0.
10. The treatment method according to claim 4, wherein the DO value is controlled to be 4.66mg/L to 5.78mg/L and the pH value is controlled to be greater than or equal to 7.0 during the secondary nitrification reaction of the wastewater.
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| CA2506038A1 (en) * | 2005-05-02 | 2006-11-02 | The University Of Western Ontario | Treatment of wastewater containing phosphorous and nitrogen |
| CN102190398A (en) * | 2010-03-12 | 2011-09-21 | 上海宝钢化工有限公司 | Coking wastewater treatment method |
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