CN117699973A - Method for treating wastewater by moving bed biomembrane reactor - Google Patents
Method for treating wastewater by moving bed biomembrane reactor Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 50
- 238000005273 aeration Methods 0.000 claims abstract description 98
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 46
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000011574 phosphorus Substances 0.000 claims abstract description 37
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 24
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 21
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 244000005700 microbiome Species 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 67
- 239000000945 filler Substances 0.000 claims description 29
- 239000010802 sludge Substances 0.000 claims description 24
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 238000012258 culturing Methods 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 241000223785 Paramecium Species 0.000 claims description 3
- 241000589516 Pseudomonas Species 0.000 claims description 3
- 230000001580 bacterial effect Effects 0.000 claims description 3
- 241000216643 Hydrogenophaga Species 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 26
- 238000010521 absorption reaction Methods 0.000 abstract description 7
- 238000006396 nitration reaction Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 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 12
- 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 12
- 230000001360 synchronised effect Effects 0.000 description 12
- 230000000694 effects Effects 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 7
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- 235000017281 sodium acetate Nutrition 0.000 description 4
- 239000001632 sodium acetate Substances 0.000 description 4
- 230000002349 favourable effect Effects 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- 241000143060 Americamysis bahia Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a method for treating wastewater by using a moving bed biomembrane reactor, which comprises the steps of placing wastewater in the reactor and performing aeration control so that microorganisms in the reactor are in an anaerobic stage, an aerobic stage and an anaerobic stage in sequence, wherein the wastewater treatment is completed after the aeration control is finished; wherein the aeration control is to stop aeration, aeration and stop aeration as one period, and the ratio of the times of stopping aeration, aeration and stopping aeration in one period is (1.8-2.2): 1 (1.8-2.2). After wastewater enters the reactor, an aeration control program is started, and microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage along with the progress of the aeration control program, so that carbon removal, nitration reaction and phosphorus absorption processes are carried out in the aerobic stage, and denitrification and phosphorus release processes are carried out in the anaerobic stage, thereby achieving the purposes of carbon removal, nitrogen removal and phosphorus removal, reducing the energy consumption of wastewater treatment, and needing no additional equipment.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a method for treating wastewater by using a moving bed biomembrane reactor.
Background
The water body is eutrophicated due to the fact that a large amount of nitrogen and phosphorus-containing substances generated by human life and production are discharged into the water body, so that aquatic plants and fish and shrimps in the water body cannot normally live and reproduce, and even human health can be indirectly influenced, therefore, the nitrogen and phosphorus wastewater needs to be treated, the treated water can be recycled or directly discharged up to the standard, and further influence on natural or human health or living environment is reduced.
Aiming at biochemical treatment of nitrogen and phosphorus wastewater, a large amount of carbon sources are needed to be added or combined with other processes in the traditional denitrification and dephosphorization process, so that the medicament cost and the investment cost are increased; compared with a plurality of tanks for traditional denitrification and dephosphorization, the synchronous nitrification and denitrification in the MBBR reactor can reduce the occupied area and equipment investment, and most of synchronous nitrification and denitrification control the dissolved oxygen at a lower concentration to promote the synchronous nitrification and denitrification, but the operation of the dissolved oxygen at the lower concentration is not easy to control, and simultaneously the carbon removal and dephosphorization effects are poor, and meanwhile, the microbial activity is low and the regeneration is slow due to lower aeration disturbance.
In view of this, the present invention has been made.
Disclosure of Invention
The invention aims to provide a method for treating wastewater by using a moving bed biofilm reactor.
The invention is realized in the following way:
in a first aspect, the present invention provides a method for treating wastewater using a moving bed biofilm reactor, wherein wastewater is placed in the reactor and aeration control is performed, so that microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage, and wastewater treatment is completed after the aeration control is completed; wherein the aeration control is to stop aeration, aeration and stop aeration as one period, and the ratio of the times of stopping aeration, aeration and stopping aeration in one period is (1.8-2.2): 1 (1.8-2.2).
In an alternative embodiment, one cycle of the aeration control is 35h-45h.
In an alternative embodiment, the dissolved oxygen concentration in the water in the aeration phase reactor is in the range of 4mg/L to 5mg/L.
In an alternative embodiment, the sludge concentration in the reactor is 3g/L to 5g/L, the pH is 7 to 8, and the temperature is 20+/-5 ℃.
In an alternative embodiment, the wastewater has a C/N <4;
preferably, the COD of the wastewater is 150mg/L-400mg/L, the total nitrogen is 50 mg/L-150 mg/L, the ammonia nitrogen is 5mg/L-20mg/L, and the total phosphorus is 2.0mg/L-5.0mg/L.
In an alternative embodiment, the concentration of the carbon source in the body of water in the reactor is 1/16g/L to 1/8g/L.
In an alternative embodiment, the biofilm culturing method in the reactor comprises:
inoculating facultative sludge into the reactor, adding artificial water to make the sludge concentration in the sludge mixed solution in the reactor be 3g/L-5g/L, and then adding filler into the reactor;
and (3) film-forming culture, namely mixing the filler, the artificial water distribution and the sludge, performing aeration control, taking the artificial water distribution, the aeration control and the water outlet as a culture period, and repeating the steps until the ammonia nitrogen removal rate is above 60%, the COD removal rate is above 80%, and finishing the biological film culture.
In an alternative embodiment, in the artificial water distribution, the mass-to-volume concentration ratio of C to N to P is (95-105): (4-6): 1, and the concentration of the P element is 2.8mg/L-3.2mg/L.
In an alternative embodiment, after the biofilm culturing is completed, observing a great number of the clockworms, the raddeana and the paramecium on the carrier under a microscope, wherein the biofilm is light yellow brown;
preferably, the filler is at least one of a biopest biological nest filler, a PE filler, and a biological curtain filler; the filling rate of the filling material in the reactor is 40% -50%;
preferably, the dominant bacterial groups in the sludge attached to the filler are pseudomonas mexico and hydrogenophaga.
In an alternative embodiment, the ratio of the wastewater in the inlet water is 15% -25% when the reactor is used for wastewater treatment for the first time, and the ratio of the wastewater in the inlet water is gradually increased according to the ratio of 15% -25% until the ratio of the wastewater in the inlet water reaches 100%.
The invention has the following beneficial effects:
after wastewater enters the reactor, an aeration control program is started, and microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage along with the progress of the aeration control program, so that carbon removal, nitration reaction and phosphorus absorption processes are carried out in the aerobic stage, and denitrification and phosphorus release processes are carried out in the anaerobic stage, thereby achieving the purposes of carbon removal, nitrogen removal and phosphorus removal, reducing the energy consumption of wastewater treatment, and needing no additional equipment.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
The embodiment of the invention provides a method for treating wastewater by using a moving bed biomembrane reactor, which comprises the steps of placing wastewater in the reactor and performing aeration control so that microorganisms in the reactor are in an anaerobic stage, an aerobic stage and an anaerobic stage in sequence, wherein the wastewater treatment is completed after the aeration control is finished; wherein the aeration control is to stop aeration, aeration and stop aeration as one period, and the ratio of the times of stopping aeration, aeration and stopping aeration in one period is (1.8-2.2): 1 (1.8-2.2).
In this embodiment, after wastewater enters the reactor, an aeration control program is started, and as the aeration control program proceeds, microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage, so that carbon removal, nitration reaction and phosphorus absorption processes are performed in the aerobic stage, and denitrification and phosphorus release processes are performed in the anaerobic stage, thereby achieving the purposes of carbon removal, nitrogen removal and phosphorus removal.
In this embodiment, a small amount of oxygen is dissolved in the water body in the reactor during a period of time when the sewage just enters the reactor and a period of time when the aeration is completed, so that even if the sewage is not aerated, a transient anoxic state exists, and thus, the microorganisms in the reactor may be in anoxic, anaerobic, aerobic, anoxic and anaerobic phases in sequence in a complete aeration control period. Wherein, denitrification and phosphorus release processes can be carried out in the anoxic stage reactor, which is still beneficial to the realization of the purposes of carbon removal, denitrification and phosphorus removal.
In this embodiment, the ratio of aeration stopping time to aeration stopping time within one period is set to be (1.8-2.2): 1 (1.8-2.2), specifically may be 1.8:1:2.2, 1.9:1:2.1, 2:1:2, 2.1:1:1.9, 2.2:1:1.8, 1.8:1.8, 1.9:1:1.9, 2.1:1:2.1, 2.2:1:2.2 or (1.8-2.2): 1 (1.8-2.2), and the allocation of aeration and aeration stopping time is favorable for reasonably allocating the times of carbon removal, digestion, denitrification, phosphorus absorption and phosphorus release, so as to achieve better wastewater purification effect, and the aeration time is relatively short in this embodiment, is favorable for reducing the running cost of the reactor.
In an alternative embodiment, one period of the aeration control is 35h-45h, specifically may be any value between 35h, 36h, 37h, 38h, 39h, 40h, 41h, 425h, 43h, 44h, 45h or 35h-45h, for example, aeration may be stopped for 16h, then aeration is stopped for 8h, aeration is stopped for 16h, one aeration control period is completed, after the reactor stably operates, after the one period, the COD removal efficiency is more than 60%, the ammonia nitrogen removal efficiency is more than 80%, the total nitrogen removal efficiency is more than 90%, and the synchronous nitrification-denitrification rate (SND rate) is about 50%; the total phosphorus removal efficiency is above 60%, the total phosphorus concentration in the effluent is always maintained in the range of 0.5mg/L-1.0mg/L, and the phosphate is discharged in the form of the shedding sludge. If the aeration control period is too short, the water treatment effect is poor, and if the aeration control period is too long, the water treatment cost is increased.
In an alternative embodiment, the dissolved oxygen concentration in the water in the aeration phase reactor is in the range of 4mg/L to 5mg/L.
The biofilm reactor has relatively good treatment effect on wastewater, but the application of the biofilm reactor is restricted by the problem that biofilm fillers are easy to block.
When the embodiment is aerated, the dissolved oxygen in the reactor is controlled at a higher concentration, so that on one hand, carbon removal, nitration and phosphorus absorption processes are facilitated, and on the other hand, higher aeration intensity is required for higher dissolved oxygen, the higher aeration intensity is favorable for improving the flowing speed of water in the reactor, so that the scouring capacity of the water to the filler is improved, the shedding and updating of microorganisms on the filler are facilitated, and further the treatment effect of the reactor on wastewater is maintained.
In alternative embodiments, the sludge concentration in the reactor is 3g/L to 5g/L, in particular may be 3g/L, 3.5g/L, 4g/L, 4.5g/L, 5g/L or any value between 3g/L and 5 g/L; a pH of 7 to 8, in particular any value between 7, 7.2, 7.4, 7.6, 7.8, 8 or 7 to 8; the temperature is 20.+ -. 5 ℃, and specifically, may be any value between 15 ℃, 17 ℃, 19 ℃, 21 ℃, 23 ℃, 25 ℃, or 20.+ -. 5 ℃.
In an alternative embodiment, the wastewater C/N <4, the wastewater treatment method in this embodiment is applicable to low C/N wastewater.
Preferably, the COD of the wastewater is 150mg/L-400mg/L, the total nitrogen is 50 mg/L-150 mg/L, the ammonia nitrogen is 5mg/L-20mg/L, and the total phosphorus is 2.0mg/L-5.0mg/L.
In alternative embodiments, the concentration of carbon source in the body of water within the reactor is in the range 1/16g/L to 1/8g/L, and may specifically be any value between 1/16, 1/14, 1/12, 1/10, 1/8 or 1/16-1/8.
In the wastewater treatment process of low C/N, a carbon source is usually required to be additionally added into a water body to serve as an electron donor, the denitrification process can be smoothly carried out only by adding an organic carbon source which is about 0.5 times that of the traditional nitrification and denitrification process after aeration is finished, both nitrate nitrogen and nitrite nitrogen in the effluent of the reactor can reach below 1.0mg/L, and a large amount of accumulation of nitrate nitrogen and nitrite nitrogen is avoided, so that compared with the traditional nitrification and denitrification process, the reagent cost is greatly reduced.
In an alternative embodiment, the biofilm culturing method in the reactor comprises:
inoculating facultative sludge into the reactor, adding artificial water to make the sludge concentration in the sludge mixed solution in the reactor be 3g/L-5g/L, and then adding filler into the reactor;
and (3) film-forming culture, namely mixing the filler, the artificial water distribution and the sludge, performing aeration control, taking the artificial water distribution, the aeration control and the water outlet as a culture period, and repeating the steps until the ammonia nitrogen removal rate is above 60%, the COD removal rate is above 80%, and finishing the biological film culture. Under normal conditions, the biofilm culture can be completed in 5 culture periods, the culture difficulty is low, and the time is relatively short.
In an alternative embodiment, in the artificial water distribution, the mass-to-volume concentration ratio of C to N to P is (95-105): (4-6): 1, and the concentration of the P element is 2.8mg/L-3.2mg/L.
The composition of the manual water distribution is adjusted, so that the requirement of microorganisms in the reactor is met, and the effect of subsequent wastewater treatment is improved. Specifically, the concentration of the P element may be 2.8mg/L, 2.9mg/L, 3.0mg/L, 3.1mg/L, 3.2mg/L or any value between 2.8mg/L and 3.2 mg/L; the concentration of N element can be 14mg/L, 14.5mg/L, 15mg/L, 15.5mg/L, 16mg/L or any value between 14mg/L and 16 mg/L; the concentration of element C may be 280mg/L, 290mg/L, 300mg/L, 310mg/L, 320mg/L or any value between 280mg/L and 320 mg/L.
In an alternative embodiment, after the biofilm culturing is completed, observing a great number of the clockworms, the raddeana and the paramecium on the carrier under a microscope, wherein the biofilm is light yellow brown;
preferably, the filler is at least one of a biopest biological nest filler, a PE filler, and a biological curtain filler; the packing fraction of the reactor internal packing is 40% -50%, in particular, may be any value between 40%, 42%, 44%, 46%, 48%, 50% or 40% -50%;
preferably, the dominant bacterial groups in the sludge attached to the filler are pseudomonas mexico and hydrogenphaga, which have denitrification effect, and the hydrogenphaga has denitrification effect, so that the effect of subsequent wastewater treatment is improved.
In an alternative embodiment, the ratio of the wastewater in the water inlet is 15% -25% when the reactor is used for wastewater treatment for the first time, the ratio of the wastewater in the water inlet is gradually increased according to the ratio of 15% -25%, until the ratio of the wastewater in the water inlet reaches 100%, the consumption of manual water distribution is gradually reduced, and a transitional effect is achieved.
The features and capabilities of the present invention are described in further detail below in connection with the examples.
Example 1
The embodiment provides a method for treating wastewater by using a moving bed biofilm reactor, which comprises the following steps:
biofilm culturing in a reactor, namely, 2 times of elutriation of facultative sludge from a Ubbelow sewage treatment plant, inoculating the facultative sludge into the reactor, and adding artificial water to enable the sludge concentration in a sludge mixed solution in the reactor to be 5g/L, and then adding BioNest biological nest filler into the reactor, wherein the filling rate, namely, the filler volume, is 50% of the total volume of the reactor; mixing the filler, the artificial water distribution and the sludge, performing aeration control to perform artificial water distribution, aeration control and water outlet as one culture period, and repeating until the ammonia nitrogen removal rate is above 60%, the COD removal rate is above 80%, and finishing the biofilm culture; wherein, in the artificial water distribution, the concentration ratio of C to N to P is 100:5:1, and the concentrations of C, N and P are 300mg/L, 15mg/L and 3mg/L respectively; aeration control comprises stopping aeration for 16h, 8h, and then stopping aeration for 16h;
and (3) wastewater treatment, namely treating the caprolactam wastewater in the coal chemical industry with C/N=3.33 and B/C=0.10, wherein the COD of the inflow water is 200mg/L, the total nitrogen is 60mg/L, the ammonia nitrogen is 5.0mg/L, and the total phosphorus is 3.0mg/L. 4L of water is fed into the reactor once, no operation is performed, namely the exposure time is stopped for 16 hours, and the denitrification process is performed; then, aeration is started, the aeration time is 8 hours, the concentration of dissolved oxygen in the water body is about 4mg/L after the concentration is stable, and the wastewater is fully contacted with the filler attached with microorganisms to carry out carbon removal, nitrification and phosphorus absorption processes; after the aeration is finished, adding 0.25g of sodium acetate into the reactor, and stopping the aeration for 16 hours; this is an operational cycle and drains after the end. After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 60mg/L, the total nitrogen is 5.0mg/L, the ammonia nitrogen is 0.8mg/L, the total phosphorus is 1.0mg/L, the nitrate nitrogen and the nitrite nitrogen are both 1.0mg/L, the SND rate is 52%, and the reactor is considered to be in the synchronous nitrification and denitrification process. After the reactor is stably operated for the 10 th period, the water quality of the effluent is detected, the COD of the effluent is 60mg/L, the total nitrogen is 5.0mg/L, the ammonia nitrogen is 1.0mg/L, the total phosphorus is 1.2mg/L, the nitrate nitrogen and the nitrite nitrogen are 1.0mg/L, the SND rate is 50%, and the reactor can be stably operated for a long time.
Comparative example 1
This comparative example provides a method for treating wastewater using a moving bed biofilm reactor, comprising:
biofilm cultivation in a reactor was as in example 1;
the wastewater treatment differs from example 1 only in that: 4L of water is fed into the reactor once, aeration is started to ensure that the concentration of dissolved oxygen is about 2mg/L, aeration is carried out for 24 hours, 0.25g of sodium acetate is added into the reactor, and aeration is continued for 16 hours. This is an operational cycle and drains after the end. After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 100mg/L, the total nitrogen is 20mg/L, the ammonia nitrogen is 2.5mg/L, the total phosphorus is 2.0mg/L, the nitrate nitrogen is 3.0mg/L, the nitrite nitrogen is 10mg/L, and the reactor does not achieve the synchronous nitrification and denitrification process. After the reactor stably operates for the 10 th period, the water quality of the effluent is detected, the COD of the effluent is 100mg/L, the total nitrogen is 25mg/L, the ammonia nitrogen is 4.0mg/L, the total phosphorus is 2.5mg/L, the nitrate nitrogen is 3.0mg/L, the nitrite nitrogen is 10mg/L, and the reactor does not achieve the synchronous nitrification and denitrification process. With the extension of the running time of the reactor, the removal effect of total nitrogen, ammonia nitrogen and total phosphorus is gradually poor.
Example 2
The embodiment provides a method for treating wastewater by using a moving bed biofilm reactor, which comprises the following steps:
biofilm cultivation in a reactor was as in example 1;
and (3) wastewater treatment, namely treating petrochemical caprolactam wastewater with C/N=2.67 and B/C=0.12, wherein the COD of the inflow water is 400mg/L, the total nitrogen is 150mg/L, the ammonia nitrogen is 15mg/L, and the total phosphorus is 5.0mg/L. 4L of water is fed into the reactor once, no operation is performed, namely the exposure time is stopped for 16 hours, and the denitrification process is performed; then, aeration is started, the aeration time is 8 hours, the concentration of dissolved oxygen in the water body is about 4mg/L after the concentration is stable, and the wastewater is fully contacted with the filler attached with microorganisms to carry out carbon removal, nitrification and phosphorus absorption processes; after the aeration is finished, adding 0.5g of sodium acetate into the reactor, and stopping the aeration for 16 hours; this is an operational cycle and drains after the end. After the reactor stably operates for the fifth period, the effluent quality is detected, the COD of the effluent is 100mg/L, the total nitrogen is 15mg/L, the ammonia nitrogen is 3.0mg/L, the total phosphorus is 2.0mg/L, the nitrate nitrogen and the nitrite nitrogen are both 2.0mg/L, the SND rate is 67%, and the reactor is considered to be in the synchronous nitrification and denitrification process. After the 10 th period of stable operation of the reactor, the water quality of the effluent is detected, the COD of the effluent is 100mg/L, the total nitrogen is 18mg/L, the ammonia nitrogen is 3.0mg/L, the total phosphorus is 2.5mg/L, the nitrate nitrogen and the nitrite nitrogen are both 2.5mg/L, the SND rate is 58%, and the reactor can stably operate for a long time.
Comparative example 2
This comparative example provides a method for treating wastewater using a moving bed biofilm reactor, comprising:
biofilm cultivation in a reactor was as in example 2;
the wastewater treatment differs from example 2 only in that: 4L of water is fed into the reactor once, aeration is started to ensure that the concentration of dissolved oxygen is about 2mg/L, aeration is carried out for 24 hours, 0.5g of sodium acetate is added into the reactor, and aeration is continued for 16 hours. This is an operational cycle and drains after the end. After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 250mg/L, the total nitrogen is 50mg/L, the ammonia nitrogen is 8.0mg/L, the total phosphorus is 4.0mg/L, the nitrate nitrogen is 5.0mg/L, the nitrite nitrogen is 15mg/L, and the reactor does not reach the synchronous nitrification and denitrification process.
Comparative example 3
The only difference from example 1 is that: in the wastewater treatment step, after water inflow in the reactor is finished, aeration is carried out for 8 hours, and aeration is stopped for 16 hours.
After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 80mg/L, the total nitrogen is 20mg/L, the ammonia nitrogen is 2.0mg/L, the total phosphorus is 2.5mg/L, the nitrate nitrogen is 5mg/L, the nitrite nitrogen is 8mg/L, and the reactor does not reach the synchronous nitrification and denitrification process.
Comparative example 4
The only difference from example 1 is that: in the wastewater treatment step, after water inflow in the reactor is finished, the aeration is stopped for 12 hours, the aeration is performed for 6 hours, and the aeration is stopped for 12 hours.
After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 80mg/L, the total nitrogen is 8.0mg/L, the ammonia nitrogen is 1.0mg/L, the total phosphorus is 2.5mg/L, the nitrate nitrogen is 2.0mg/L, the nitrite nitrogen is 2.0mg/L, and the reactor does not achieve the synchronous nitrification and denitrification process.
Comparative example 5
The only difference from example 1 is that: in the wastewater treatment step, after water inflow in the reactor is finished, the aeration is stopped for 10 hours, the aeration is performed for 20 hours, and the aeration is stopped for 10 hours.
After the reactor stably operates for the fifth period, the water quality of the effluent is detected, the COD of the effluent is 70mg/L, the total nitrogen is 6.0mg/L, the ammonia nitrogen is 1.0mg/L, the total phosphorus is 1.5mg/L, the nitrate nitrogen is 2.0mg/L and the nitrite nitrogen is 1.0mg/L, and the reactor does not reach the synchronous nitrification and denitrification process.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for treating wastewater by using a moving bed biofilm reactor is characterized in that the wastewater is placed in the reactor and is subjected to aeration control, so that microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage, and the wastewater treatment is completed after the aeration control is finished; wherein the aeration control is to stop aeration, aeration and stop aeration as one period, and the ratio of the times of stopping aeration, aeration and stopping aeration in one period is (1.8-2.2): 1 (1.8-2.2).
2. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein one period of aeration control is 35h to 45h.
3. The method for treating wastewater by using a moving bed biofilm reactor according to claim 1, wherein the concentration of dissolved oxygen in the water body in the reactor in the aeration stage is 4mg/L to 5mg/L.
4. The method for treating wastewater by using a moving bed biofilm reactor according to claim 1, wherein the concentration of sludge in the reactor is 3g/L to 5g/L, the pH is 7 to 8, and the temperature is 20+/-5 ℃.
5. The method of treating wastewater with a moving bed biofilm reactor according to claim 1, wherein the wastewater has a C/N <4;
preferably, the COD of the wastewater is 150mg/L-400mg/L, the total nitrogen is 50 mg/L-150 mg/L, the ammonia nitrogen is 5mg/L-20mg/L, and the total phosphorus is 2.0mg/L-5.0mg/L.
6. The method for treating wastewater by using a moving bed biofilm reactor according to claim 1, wherein the concentration of carbon source in the water body in the reactor is 1/16g/L to 1/8g/L.
7. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein the biofilm culturing method in the reactor comprises:
inoculating facultative sludge into the reactor, adding artificial water to make the sludge concentration in the sludge mixed solution in the reactor be 3g/L-5g/L, and then adding filler into the reactor;
and (3) film-forming culture, namely mixing the filler, the artificial water distribution and the sludge, performing aeration control, taking the artificial water distribution, the aeration control and the water outlet as a culture period, and repeating the steps until the ammonia nitrogen removal rate is above 60%, the COD removal rate is above 80%, and finishing the biological film culture.
8. The method for treating wastewater by using a moving bed biofilm reactor according to claim 7, wherein in the artificial water distribution, the mass-volume concentration ratio of CN to P is (95-105): (4-6): 1, and the concentration of the P element is 2.8mg/L-3.2mg/L.
9. The method for treating wastewater by using a moving bed biofilm reactor according to claim 7, wherein after the biofilm culturing is completed, observing that a great amount of clockworm, raddeana and paramecium are on a carrier under a microscope, and the biofilm is light yellow brown;
preferably, the filler is at least one of a biopest biological nest filler, a PE filler, and a biological curtain filler; the filling rate of the filling material in the reactor is 40% -50%;
preferably, the dominant bacterial groups in the sludge attached to the filler are pseudomonas mexico and hydrogenophaga.
10. The method for treating wastewater by using a moving bed biofilm reactor according to claim 1, wherein the ratio of wastewater in the inlet water is 15% -25% when the reactor is used for wastewater treatment for the first time, and the ratio of wastewater in the inlet water is gradually increased according to the ratio of 15% -25% until the ratio of wastewater in the inlet water reaches 100%.
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