CN115043489A - Method for enhancing single-stage autotrophic nitrogen removal performance - Google Patents
Method for enhancing single-stage autotrophic nitrogen removal performance Download PDFInfo
- Publication number
- CN115043489A CN115043489A CN202210639225.6A CN202210639225A CN115043489A CN 115043489 A CN115043489 A CN 115043489A CN 202210639225 A CN202210639225 A CN 202210639225A CN 115043489 A CN115043489 A CN 115043489A
- Authority
- CN
- China
- Prior art keywords
- reactor
- nitrogen removal
- performance
- enhancing
- stage
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 37
- 230000001651 autotrophic effect Effects 0.000 title claims abstract description 27
- 230000002708 enhancing effect Effects 0.000 title claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 59
- 239000010802 sludge Substances 0.000 claims abstract description 55
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 22
- 239000011574 phosphorus Substances 0.000 claims abstract description 22
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000014759 maintenance of location Effects 0.000 claims abstract description 20
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 20
- 239000001301 oxygen Substances 0.000 claims abstract description 20
- 239000011573 trace mineral Substances 0.000 claims description 16
- 235000013619 trace mineral Nutrition 0.000 claims description 16
- 238000005273 aeration Methods 0.000 claims description 7
- 230000032770 biofilm formation Effects 0.000 claims description 5
- 159000000007 calcium salts Chemical class 0.000 claims description 4
- 159000000003 magnesium salts Chemical class 0.000 claims description 4
- 238000005728 strengthening Methods 0.000 claims description 4
- 239000008399 tap water Substances 0.000 claims description 4
- 235000020679 tap water Nutrition 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 claims description 3
- 201000006747 infectious mononucleosis Diseases 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 2
- 230000001376 precipitating effect Effects 0.000 claims description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical class OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 25
- 238000006243 chemical reaction Methods 0.000 abstract description 23
- 241001453382 Nitrosomonadales Species 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 239000012528 membrane Substances 0.000 abstract description 5
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 12
- 241000894006 Bacteria Species 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- 239000000945 filler Substances 0.000 description 9
- 238000009826 distribution Methods 0.000 description 7
- 244000005700 microbiome Species 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 6
- 241000108664 Nitrobacteria Species 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 4
- VGPSUIRIPDYGFV-UHFFFAOYSA-N [N].O[N+]([O-])=O Chemical compound [N].O[N+]([O-])=O VGPSUIRIPDYGFV-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000004060 metabolic process Effects 0.000 description 3
- 230000036284 oxygen consumption Effects 0.000 description 3
- 229920000728 polyester Polymers 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 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 2
- 230000009471 action Effects 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 150000001868 cobalt Chemical class 0.000 description 2
- 150000001879 copper Chemical class 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000011081 inoculation Methods 0.000 description 2
- 150000002696 manganese Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000002572 peristaltic effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 150000003751 zinc Chemical class 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 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
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 210000000170 cell membrane Anatomy 0.000 description 1
- 210000003850 cellular structure Anatomy 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- 159000000014 iron salts Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009935 nitrosation Effects 0.000 description 1
- 238000007034 nitrosation reaction Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- DJFBJKSMACBYBD-UHFFFAOYSA-N phosphane;hydrate Chemical compound O.P DJFBJKSMACBYBD-UHFFFAOYSA-N 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000003307 slaughter Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000031068 symbiosis, encompassing mutualism through parasitism Effects 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000004102 tricarboxylic acid cycle Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
Images
Classifications
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to the technical field of wastewater treatment, and particularly relates to a method for enhancing single-stage autotrophic nitrogen removal performance. In the two different stages of starting and stably operating the reactor, parameters such as the temperature, the dissolved oxygen concentration, the hydraulic retention time, the pH value of inlet water, the phosphorus concentration and the like of a system in the biological filter reactor are respectively adjusted, and the parameters are controlled within proper ranges, so that aerobic ammonia oxidizing bacteria are enriched on the surface of a biological membrane of the reactor in the operating stage, and anaerobic ammonia oxidizing bacteria are enriched in the biological membrane in the operating stage, thereby obviously improving the denitrification performance of the biological filter reactor, wherein the ammonia-nitrogen conversion rate can reach 96.3% during starting, and the total nitrogen removal rate can reach 70.0%; during operation, the ammonia-nitrogen conversion rate is 90.6-100.0%, and the total nitrogen removal rate is 77.0-98.4%. The invention does not need to discharge sludge in the whole process during the startup and operation of the reactor, does not need to add an organic carbon source, and greatly reduces the operation cost.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a method for enhancing single-stage autotrophic nitrogen removal performance.
Background
The industries of pharmaceutical chemistry, chemical fertilizer, petrifaction, coking, smelting, slaughtering and the like are industrial households discharging ammonia nitrogen-containing wastewater in China, and the discharged high-concentration ammonia nitrogen wastewater has the characteristic of low C/N ratio and belongs to one of the main industrial wastewater which is difficult to treat. When the traditional biological denitrification nitrification-denitrification technology is adopted to treat the wastewater, the actual problems that the nitrification effect of high ammonia nitrogen load is poor and a large amount of organic carbon sources are required to be added in the denitrification exist. In addition, the traditional technology also has the technical bottlenecks of long process flow, high energy consumption and drug consumption, high residual sludge yield and the like, so that the traditional biological denitrification technology of nitrification and denitrification is not suitable for the effective treatment of wastewater with high-concentration ammonia nitrogen and low C/N ratio.
The single-stage autotrophic nitrogen removal technology has the characteristics of saving 62.5 percent of oxygen consumption, saving 100 percent of organic carbon source and 50 percent of alkali consumption, having short process flow, little sludge production and the like, and becomes a popular novel biological nitrogen removal technology at present. The technology is characterized in that a half amount of nitrosation and anaerobic ammonium oxidation reaction is simultaneously realized in an integrated reactor, specifically, half amount of ammonia nitrogen is oxidized into nitrite nitrogen under the action of aerobic ammonium oxidation bacteria; the generated nitrite nitrogen and the residual ammonia nitrogen react under the action of anaerobic ammonia oxidizing bacteria to generate nitrogen and generate a small amount of nitrate nitrogen, thereby realizing the effective removal of the ammonia nitrogen from the wastewater. However, functional bacteria in the system, namely aerobic ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria, are very sensitive to water quality conditions and environmental factors, so that the technical problem of unstable operation of single-stage autotrophic nitrogen removal often occurs, and the application of the technology in practical engineering is influenced.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, and provides a method for strengthening the single-stage autotrophic nitrogen removal performance, which effectively improves the operation stability of a biological filter reactor and improves the biological nitrogen removal performance of the biological filter reactor.
In order to realize the purpose, the technical scheme adopted by the invention is as follows:
the invention provides a method for strengthening the performance of single-stage autotrophic nitrogen removal, which comprises the following steps:
(1) inoculating the seed sludge into a biological filter reactor;
(2) introducing inert gas into the biological filter reactor until the biological biofilm formation of the reactor is successful;
(3) continuously feeding inlet water into a biofilter reactor with successful biofilm formation, and aerating from the bottom of the biofilter reactor until the reactor is successfully started;
(4) and continuously feeding the inlet water into the biological filter reactor which is successfully started, and simultaneously aerating from the bottom of the biological filter reactor to ensure that the biological filter reactor stably operates.
Preferably, the biofilter reactor is a submerged biofilter reactor.
The conventional biological denitrification technology is a combined nitrification-denitrification method, and in actual operation, the conventional problems of limited denitrification capacity, long process flow, high oxygen consumption and organic carbon source demand, high residual sludge yield and the like exist, so that the treatment effect of the nitrification-denitrification integrated biochemical technology on the ammonia nitrogen-containing wastewater is limited. Compared with the conventional biological denitrification technology, the method provided by the invention can be used for performing single-stage autotrophic denitrification in one reactor, so that the total nitrogen removal is effectively realized. Saves the oxygen consumption by 62.5 percent, the organic carbon source of 100 percent and the alkali consumption by 50 percent, reduces the process flow by half and reduces the sludge production, which shows the advantages of single-stage autotrophic nitrogen removal on the technology and the economy. Researches show that the dissolved oxygen concentration, the pH value, the temperature, the hydraulic retention time and the phosphorus concentration of inlet water of a system in the reactor are all key factors influencing the denitrification performance of the biological filter reactor. Wherein, the pH value can change the surface charge of cell membranes, thereby influencing the absorption of nutrient substances by microorganisms and the activity of enzymes in the metabolic process of the microorganisms; the dissolved oxygen is a key factor for the synergistic symbiosis of functional bacteria (aerobic ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria) in a balanced reaction system; temperature is an important factor affecting the activity and protein properties of enzymes within the microorganism; phosphorus is one of the cell components in the body of the microorganism and influences the anabolism of the microorganism through the tricarboxylic acid cycle; the hydraulic retention time controls different metabolism periods of the microorganism in the reaction system. These factors all have a significant impact on the ammonia nitrogen conversion and total nitrogen removal of the system; therefore, it is necessary and valuable to enhance the performance of single-stage autotrophic nitrogen removal and effectively optimize the operation cost by optimizing the process parameters such as the concentration of dissolved oxygen, the pH value, the temperature, the concentration of phosphorus in the feed water, the hydraulic retention time and the like in the system at the start-up and operation stages of the reactor.
Preferably, in the step (3), the dissolved oxygen concentration of the system in the biological filter reactor is 0.3-1.9 mg/L, the pH value is 6.7-8.0, the water temperature is 30-31.5 ℃, and the hydraulic retention time is 22-24 h.
Preferably, in the step (3), the phosphorus concentration of the inlet water is 5.6-8.0 mg/L.
In the invention, the step (3) is a starting stage of the biological filter reactor, and parameters such as temperature, dissolved oxygen, pH value, hydraulic retention time, phosphorus concentration in inlet water and the like in the system are controlled in a proper range in the starting stage, so that the activity and growth of nitrobacteria can be effectively inhibited, the growth and enrichment of functional bacteria aerobic ammonia oxidizing bacteria are promoted, more functional bacteria aerobic ammonia oxidizing bacteria are enriched on the surface of a biological membrane of the reactor, the promotion effect on the promotion of the single-stage autotrophic nitrogen removal performance is obvious, and sludge discharge is not required in the stage. The ammonia nitrogen conversion rate of the effluent is not less than 90.0 percent, and the total nitrogen removal rate is not less than 70.0 percent, namely the reactor is considered to be successfully started.
Preferably, in the step (4), the dissolved oxygen concentration of the system in the reactor is 0.6-0.8 mg/L, the pH value is 6.2-8.2, the water temperature is 29-33 ℃, and the hydraulic retention time is 22-24 hours.
Preferably, in the step (4), the phosphorus concentration of the inlet water is 4.5-8.0 mg/L.
In the invention, the step (4) is a stable operation stage of the biological filter reactor. At this stage, parameters such as temperature, dissolved oxygen, pH value, hydraulic retention time, phosphorus concentration in inlet water and the like in the system are controlled within a proper range, so that the functional bacteria anammox bacteria are enriched in the biofilm at the operation stage. No sludge discharge is required during the stable operation phase. The ammonia-nitrogen conversion rate of the biological filter reactor is 90.6-100%, the total nitrogen removal rate is 77.0-98.4%, and the reactor can be considered to be operated successfully and stably.
Preferably, the inlet water is prepared from a nitrogen source, a phosphorus source, a soluble magnesium salt, a soluble calcium salt, a soluble bicarbonate, a trace element solution and tap water.
Further preferably, each liter of the artificial water distribution comprises: 0.38-0.63 g of nitrogen source, 0.03-0.05 g of phosphorus source, 0.01-0.02 g of soluble magnesium salt, 0.01-0.02 g of soluble calcium salt, 0.80-1.00 g of soluble bicarbonate and 0.25-0.30 mL of trace element solution.
More preferably, the trace elements in the trace element solution are at least one selected from soluble iron salts, soluble manganese salts, soluble copper salts, soluble zinc salts and soluble cobalt salts.
Still more preferably, the trace element solution comprises, per liter: 3.00 to 3.50g of soluble iron salt, 0.30 to 0.40g of soluble manganese salt, 0.07 to 0.08g of soluble copper salt, 0.02 to 0.30g of soluble zinc salt and 0.30 to 0.40g of soluble cobalt salt.
Preferably, the seed mud is prepared by the following method: precipitating the activated sludge, and carrying out aeration treatment on the precipitated activated sludge to obtain seed sludge.
Preferably, the pH value of the activated sludge is 6.6-7.4, and the sludge concentration of the activated sludge is 1500-2500 mg/L.
Further preferably, the sludge concentration of the activated sludge after precipitation is 12000-14000 mg/L, and the volatile sludge concentration is 4500-5000 mg/L.
Further preferably, the time of the precipitation treatment is 4-8 hours, and the time of the aeration treatment is 20-30 hours.
Preferably, the sludge concentration of the seed sludge is 18000-22000 mg/L, and the volatile sludge concentration (MLVSS) is 4500-5000 mg/L.
Preferably, the ratio of the inoculation volume of the seed sludge to the effective volume of the biofilter reactor is 1 (2-4).
Preferably, the step (2) specifically comprises: and continuously ventilating the bottom of the biological filter reactor, maintaining the air pressure in the reactor at 0.2-0.3 MPa, gradually attaching the sludge in the reactor to the surface of the filler, successfully biofilm-culturing the reactor when the color of the sludge attached to the filler is changed from light yellow brown to black brown, stopping ventilation, standing, and discharging the residual sludge at the bottom of the reactor.
Further preferably, the continuous aeration time is 48-72 hours, and the standing time is 4-8 hours.
Compared with the prior art, the invention has the beneficial effects that:
(1) in the two different stages of starting and stably operating the reactor, parameters such as the temperature, the dissolved oxygen concentration, the hydraulic retention time, the pH value of inlet water, the phosphorus concentration and the like of a system in the biological filter reactor are respectively adjusted, and the parameters are controlled within proper ranges, so that the aerobic ammonia oxidizing bacteria of the functional bacteria are enriched on the surface of a biological film of the reactor in the operating stage, and the anaerobic ammonia oxidizing bacteria of the functional bacteria are enriched in the biological film in the operating stage, thereby obviously improving the denitrification performance of the biological filter reactor, wherein during the starting period, the ammonia-nitrogen conversion rate is improved from 22.7 percent to 96.3 percent, and the total nitrogen removal rate is improved from 0.0 percent to 70.0 percent; during the run, the ammonia-nitrogen conversion was 90.6-100.0%, the average conversion was 95.5%, the total nitrogen removal was 77.0-98.4%, and the average removal was 87.3%.
(2) Aiming at different requirements of the two stages of starting and stable operation of the reactor on condition parameter ranges, the method respectively adjusts the temperature, the dissolved oxygen concentration, the pH value and the hydraulic retention time of the system in the reactor, has larger threshold value range of each parameter, improves the denitrification performance of the reactor by combining the optimized control of the phosphorus concentration of inlet water, is easy to operate, and is more beneficial to the wide application of the method.
(3) The invention does not need to discharge sludge in the whole process during the startup and operation of the reactor, does not need to add an organic carbon source, and greatly reduces the operation cost.
Drawings
FIG. 1 is a graph showing the variation of the nitrogen concentration and phosphorus concentration of each system in a reactor during a start-up period and a run-time period;
FIG. 2 is a graph of ammonia nitrogen conversion and total nitrogen removal over start-up and run-time.
Detailed Description
To better illustrate the objects, aspects and advantages of the present invention, the present invention will be further described with reference to specific examples. It will be understood by those skilled in the art that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The reagents, methods and equipment adopted by the invention are conventional in the technical field if no special description is given.
Example 1
The embodiment provides a method for enhancing the performance of single-stage autotrophic nitrogen removal, which comprises the following steps:
(1) preparing seed mud: taking activated sludge with the pH value of 6.6-7.4 as seed sludge, wherein the sludge concentration (MLSS) of the activated sludge is 1500-2500 mg/L, and performing precipitation treatment for 4-8 hours to obtain the seed sludge, wherein the sludge concentration (MLSS) in the seed sludge is 12000-14000 mg/L, and the volatile sludge concentration (MLVSS) is 4500-5000 mg/L;
(2) inoculating seed sludge: performing air aeration on the seed sludge subjected to precipitation in the step (1), adjusting the sludge concentration of the seed sludge to 18000-22000 mg/L to obtain adjusted sludge, then pouring the adjusted sludge into a submerged biological filter (SBAF) reactor, wherein the ratio of the volume of the adjusted sludge to the effective volume of the SBAF reactor is 1:3, a combined filler component is arranged in the submerged biological filter (SBAF) reactor, the combined filler component comprises single filler pieces, a plastic sleeve and a central copper pipe wire, the single filler pieces are arranged in parallel, the plastic sleeve penetrates through holes in the single filler pieces, the plastic sleeve and the single filler pieces are fixedly connected through the central copper pipe wire, the plastic sleeve comprises an inner ring plastic ring and an outer ring plastic ring, the plastic ring is formed by pressing and buckling plastic circular sheets, and polyester fibers are arranged between the inner ring plastic ring and the outer ring plastic ring, the fiber bundles of the polyester yarns are uniformly distributed, and the inner ring plastic rings and the outer ring plastic rings are snowflake-shaped plastic branches, so that the polyester yarns can be used for hanging membranes and effectively cutting bubbles, the transfer rate and the utilization rate of oxygen are improved, water and gas are fully exchanged through a biological membrane, and further nitrogen in water is efficiently treated;
(3) biological biofilm formation: introducing nitrogen to the bottom of the SBAF reactor, controlling the air pressure in the SBAF reactor to be 0.2-0.3 MPa, continuously introducing the nitrogen for 48-72 hours, stopping introducing the nitrogen when sludge in the reactor is gradually attached to the surface of the combined filler and the color of the sludge is changed from light yellow brown to black brown, standing for 4-6 hours, and discharging residual sludge from a sludge discharge port at the bottom of the reactor;
(4) starting and operating: feeding inlet water into an SBAF reactor which is successfully coated with a film by using a peristaltic pump, carrying out micro-aerobic aeration from the bottom of the reactor, controlling the dissolved oxygen concentration (DO) of a system in the reactor to be 0.3-1.9 mg/L, controlling the pH value to be 6.7-8.0, controlling the water temperature to be 30.0-31.5 ℃, and controlling the hydraulic retention time to be 22-24 h so as to ensure the nutritional requirements of the growth and metabolism of microorganisms;
during start-up operation, the feed water is NH 4 Cl、KH 2 PO 4 、MgSO 4 、CaCl 2 、NaHCO 3 And the trace element solution is dissolved in tap water to prepare artificial water distribution, and each liter of artificial water distribution comprises: NH (NH) 4 Cl 0.38～0.63g、KH 2 PO 4 ·3H 2 O 0.035～0.05g、MgSO 4 0.01～0.02g、CaCl 2 0.01～0.02g、 NaHCO 3 0.80-1.00 g, 0.25-0.30 mL of microelement solution; wherein each liter of the trace element solution comprises: FeCl 3 ·6H 2 O 3.00～3.50g、MnCl 2 ·4H 2 O 0.30～0.40g、CuSO 4 ·5H 2 O 0.07～0.08g、ZnSO 4 ·7H 2 O 0.02～0.30g、CoCl 2 ·6H 2 And 0.30-0.40 g of O, performing water quality detection on inlet water and outlet water of the reactor every day, and calculating the ammonia nitrogen conversion rate and the total nitrogen removal rate, wherein the detection results are shown in table 1 and figures 1-2.
TABLE 1 quality of inlet and outlet water and parameters of reaction system (1 st-39 d, during system startup period)
As can be seen from Table 1 and FIGS. 1 to 2, from day 1 to 9 of the start, the sludge was in the initial stage of inoculation, and the low DO severely inhibited the activities of the aerobic ammonia-oxidizing bacteria and the nitrifying bacteria, resulting in most of NH 4 + N is not oxidized, yielding NH 4 + The N concentration is within the range of 72.0-116.0 mg/L, and the average mass concentration is 94.0 mg/L; NO of effluent 2 - The N concentration is within the range of 6.0-53.0 mg/L, and the average mass concentration is 23.4 mg/L; NO of effluent 3 - -N concentration in the range of 0.7-3.1mg/L, average mass concentration of 2.0 mg/L; in 10-27 days, a large amount of aerobic ammonia oxidizing bacteria and a small amount of nitrobacteria exist in the system, and NH in effluent is caused 4 + The mass concentration of-N is reduced from 96.0mg/L to 33.0mg/L, and the effluent NO is 2 - The mass concentration of N is increased from 15.0mg/L to 55.0 mg/L; NO of effluent 3 - The mass concentration of N is increased from 1.1mg/L to 7.2mg/L, which shows that the nitrobacteria can be effectively inhibited. From 28 th to 38 th, the system is continuously enriched with aerobic ammonia oxidizing bacteria and begins to be enriched with anaerobic ammonia oxidizing bacteria to cause an anaerobic ammonia oxidizing phenomenon, wherein the effluent NH 4 + The concentration of-N is reduced from 33.0mg/L to 6.0mg/L, and NO is discharged 2 - -the N concentration is reduced from 55.0mg/L to 40.0 mg/L; at the same time, the effluent NO 3 - The mass concentration of N is within the range of 3.0-9.3 mg/L; at 39d of reactor operation, water NH is discharged 4 + The concentration of-N is 6.0mg/L, and the effluent NO 2 - The concentration of-N is 16.0mg/L, and the effluent NO 3 - The mass concentration of N is 8.0mg/L, the process does not discharge sludge, and the start-up success of the SBAF reactor is indicated when the ammonia nitrogen conversion rate exceeds 90.0% and the total nitrogen removal rate exceeds 70.0%.
(6) And (3) stable operation: continuously feeding inlet water into an SBAF reactor which is successfully started by using a peristaltic pump, carrying out micro-aerobic aeration from the bottom of the reactor, adjusting DO of a reaction system to be within a range of 0.6-0.8 mg/L, controlling the pH value to be within a range of 6.2-8.2, controlling the water temperature to be within a range of 29.3-32.2 ℃, controlling the hydraulic retention time to be within a range of 22-24 h, and controlling the concentration of inlet water phosphorus to be within a range of 4.5-8.0 mg/L;
in the stable operation stage, the feed water is NH 4 Cl、KH 2 PO 4 、MgSO 4 、CaCl 2 、NaHCO 3 And the trace element solution is dissolved in tap water to prepare artificial water distribution, and each liter of artificial water distribution comprises: NH (NH) 4 Cl 0.38～0.63g、KH 2 PO 4 ·3H 2 O 0.03～0.05g、MgSO 4 0.01～0.02g、CaCl 2 0.01～0.02g、 NaHCO 3 0.80-1.00 g of trace element solution and 0.25-0.30 mL of trace element solution; wherein each liter of the trace element solution comprises: FeCl 3 ·6H 2 O 3.00～3.50g、MnCl 2 ·4H 2 O 0.30～0.40g、CuSO 4 ·5H 2 O 0.07～0.08g、ZnSO 4 ·7H 2 O 0.02～0.30g、CoCl 2 ·6H 2 O 0.30～0.40g，
During the stable operation, the water quality of inlet water and outlet water of the reactor is detected every day, the ammonia nitrogen conversion rate and the total nitrogen removal rate are calculated, and the detection results are shown in table 2 and fig. 1-2.
TABLE 2 quality of inlet and outlet water and parameter table of reaction system (40 th-151 th, during steady operation)
As can be seen from Table 2 and FIGS. 1-2, after the system enters the operation stage, water NH is fed in the 40 th to 151 th days 4 + The mass concentration of N is within the range of 102.0-165.0 mg/L, and the average mass concentration is 142.8 mg/L; outlet water NH 4 + The mass concentration of N is within the range of 0.0-15.0 mg/L, and the average mass concentration is 5.9 mg/L; NO of effluent 2 - -the mass concentration of N is in the range of 0.0-17.0 mg/L, and the average mass concentration is 5.1 mg/L; outlet water NH 4 + -N and NO 2 - The mass concentration of-N is kept at a low level. NO of effluent 3 - The mass concentration of-N is within the range of 1.9-21.0 mg/LThe average mass concentration of the interior and the exterior is 6.9mg/L, which shows that the content of nitrobacteria in the system is extremely low. In the operation stage, the ammonia-nitrogen conversion rate is within 89.4-100.0%, and the average conversion rate is 95.4%; the total nitrogen removal rate is within the range of 77.0-98.4%, and the average removal rate is 87.0%.
In this example, the reactor system was operated continuously and stably during start-up and steady operation without sludge discharge and without the addition of organic carbon source, which fully confirms that mono-stage autotrophic nitrogen removal is a contributor to total nitrogen removal in the system.
Comparative example 1
The comparative example provides a whole autotrophic nitrogen removal starting operation method, and is different from the embodiment 1 in that the water temperature, the oxygen content, the pH value and the hydraulic retention time of the comparative example in the whole starting and running processes are shown in a table 3, the water inflow of the comparative example in the whole starting and running processes is artificial water distribution, and each liter of the artificial water distribution comprises the following steps: NH (NH) 4 Cl 0.38～0.63g、KH 2 PO 4 ·3H 2 O 0.03～0.05g、MgSO 4 0.01～0.02g、CaCl 2 0.01～0.02g、NaHCO 3 0.80-1.00 g of trace element solution and 0.25-0.30 mL of trace element solution; wherein each liter of the trace element solution comprises the following components: FeCl 3 ·6H 2 O 3.00～3.50g、MnCl 2 ·4H 2 O 0.30～0.40g、CuSO 4 ·5H 2 O 0.07～0.08g、ZnSO 4 ·7H 2 O 0.02～0.30g、CoCl 2 ·6H 2 O 0.30～0.40g。
TABLE 3 comparison of various parameters
As can be seen from the embodiment 1 and the comparative example 1, in the starting and the operation of the conventional single-stage autotrophic nitrogen removal in the comparative example 1, the ammonia nitrogen conversion rate is controlled to be 80-90% and the total nitrogen removal rate is controlled to be 50-80% by adopting the modes of controlling the temperature, the dissolved oxygen, the ammonia nitrogen load of the inlet water, the hydraulic retention time and the like. In the embodiment 1, in two different stages of system starting and stable operation, parameters of temperature, dissolved oxygen concentration, pH value and hydraulic retention time in a system are respectively adjusted, and the phosphorus concentration of inlet water of the system is adjusted and controlled within the range of 4.5-8.0 mg/L, wherein in the starting operation stage, the phosphorus concentration of the inlet water is controlled within the range of 5.6-8.0 mg/L; and in the stable operation stage, the phosphorus concentration of the inlet water is controlled within the range of 4.5-8.0 mg/L. During the start-up run, the ammonia-nitrogen conversion was increased from 22.7% to 96.3% and the total nitrogen removal was increased from 0.0% to 70.0%. In the stable operation stage, the ammonia-nitrogen conversion rate is 90.6-100.0%, the average conversion rate is 95.5%, the total nitrogen removal rate is 77.0-98.4%, and the average removal rate is 87.3%, which technically shows the superiority of the method.
During the operation of the reactor of the comparative example 1, the concentration of the effluent nitric acid nitrogen gradually rises due to the gradual accumulation of nitrifying bacteria, and the concentration of the effluent nitric acid nitrogen varies within 10-30 mg/L, and often exceeds 20mg/L, which affects the total nitrogen removal performance of the reactor of the comparative example 1. In the embodiment 1, in two stages of the starting and the stable operation of the reactor, the temperature, the dissolved oxygen concentration, the pH value and the hydraulic retention time of a system in the reactor are respectively subjected to parameter adjustment, and the optimized control of the phosphorus concentration of inlet water is added, so that the activity and the growth of nitrobacteria can be effectively inhibited, the average concentration of nitric acid nitrogen in outlet water is lower than 7.1mg/L, and the promotion effect on the improvement of the single-stage autotrophic nitrogen removal performance is remarkable.
Comparative example 1 the critical conditions of the temperature, dissolved oxygen concentration, influent ammonia nitrogen load, hydraulic retention time and the like of the system in the reactor are controlled within a very strict and narrow threshold range in the startup and operation stage of the reactor, which has very high requirements on the design precision of the automatic control equipment in the actual engineering and the skill level of the operators. The embodiment 1 aims at different requirements of two stages of reactor starting and stable operation on condition parameter ranges, the temperature, the dissolved oxygen concentration, the pH value and the hydraulic retention time of a system in the reactor are respectively subjected to parameter adjustment, the threshold value range of each parameter is large, and the denitrification performance of the reactor is improved by combining the optimized control on the phosphorus concentration of inlet water, so that the method has more practical and effective feasibility for design and control of automatic control equipment and the skill level of operators in actual engineering, and is more beneficial to the wide application of the technology.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention is described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (10)
1. A method for strengthening the performance of single-stage autotrophic nitrogen removal is characterized by comprising the following steps:
(1) inoculating the seed sludge into a biological filter reactor;
(2) introducing inert gas into the biological filter reactor until the biological biofilm formation of the reactor is successful;
(3) continuously feeding inlet water into a biofilter reactor with successful biofilm formation, and aerating from the bottom of the biofilter reactor until the reactor is successfully started;
(4) and continuously feeding inlet water into the successfully started biological filter reactor, and simultaneously aerating from the bottom of the biological filter reactor to ensure that the biological filter reactor stably operates.
2. The method of enhancing the performance of single-stage autotrophic nitrogen removal according to claim 1, wherein said biofilter reactor is a submerged biofilter reactor.
3. The method for enhancing the performance of single-stage autotrophic nitrogen removal according to claim 1, wherein in the step (3), the dissolved oxygen concentration of the system in the biofilter reactor is 0.3-1.9 mg/L, the pH value is 6.7-8.0, the water temperature is 30-31.5 ℃, and the hydraulic retention time is 22-24 h.
4. The method for enhancing the performance of single-stage autotrophic nitrogen removal according to claim 1, wherein in the step (3), the phosphorus concentration of the feed water is 5.6-8.0 mg/L.
5. The method for enhancing the performance of single-stage autotrophic nitrogen removal according to claim 1, wherein in the step (4), the dissolved oxygen concentration of the system in the biofilter reactor is 0.6-0.8 mg/L, the pH value is 6.2-8.2, the water temperature is 29-33 ℃, and the hydraulic retention time is 22-24 h.
6. The method for enhancing the performance of single-stage autotrophic nitrogen removal according to claim 1, wherein in the step (4), the phosphorus concentration of the feed water is 4.5-8.0 mg/L.
7. The method of enhancing the performance of one-stage autotrophic nitrogen removal according to claim 1, wherein said influent water is formulated from a nitrogen source, a phosphorus source, soluble magnesium salts, soluble calcium salts, soluble bicarbonate salts, trace elements solutions, and tap water.
8. The method of enhancing mono-stage autotrophic nitrogen removal performance of claim 1, wherein said influent water comprises: 0.38-0.63 g/L of nitrogen source, 0.03-0.05 g of phosphorus source, 0.01-0.02 g/L of soluble magnesium salt, 0.01-0.02 g/L of soluble calcium salt, 0.80-1.00 g/L of soluble bicarbonate and 0.25-0.30 ml/L of trace element solution.
9. The method of enhancing mono-stage autotrophic nitrogen removal according to claim 1, wherein said seed sludge is produced by the following method: and (3) precipitating the activated sludge, and carrying out aeration treatment on the precipitated activated sludge to obtain seed sludge.
10. The method for enhancing the single-stage autotrophic nitrogen removal performance of claim 1, wherein the seed sludge has a sludge concentration of 18000-22000 mg/L and a volatile sludge concentration of 4500-5000 mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210639225.6A CN115043489B (en) | 2022-06-07 | 2022-06-07 | Method for strengthening single-stage autotrophic denitrification performance |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210639225.6A CN115043489B (en) | 2022-06-07 | 2022-06-07 | Method for strengthening single-stage autotrophic denitrification performance |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115043489A true CN115043489A (en) | 2022-09-13 |
| CN115043489B CN115043489B (en) | 2024-02-27 |
Family
ID=83160973
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210639225.6A Active CN115043489B (en) | 2022-06-07 | 2022-06-07 | Method for strengthening single-stage autotrophic denitrification performance |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115043489B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101618911A (en) * | 2009-07-23 | 2010-01-06 | 重庆大学 | Method of realizing one-step autotrophic nitrogen removal under higher levels of dissolved oxygen |
| CN103193320A (en) * | 2013-03-17 | 2013-07-10 | 北京工业大学 | Efficient autotrophic denitrification method of bacterial filter |
| CN106542636B (en) * | 2016-10-28 | 2019-07-26 | 广州中国科学院沈阳自动化研究所分所 | A kind of method of quick start whole process autotrophic denitrification |
-
2022
- 2022-06-07 CN CN202210639225.6A patent/CN115043489B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101618911A (en) * | 2009-07-23 | 2010-01-06 | 重庆大学 | Method of realizing one-step autotrophic nitrogen removal under higher levels of dissolved oxygen |
| CN103193320A (en) * | 2013-03-17 | 2013-07-10 | 北京工业大学 | Efficient autotrophic denitrification method of bacterial filter |
| CN106542636B (en) * | 2016-10-28 | 2019-07-26 | 广州中国科学院沈阳自动化研究所分所 | A kind of method of quick start whole process autotrophic denitrification |
Non-Patent Citations (1)
| Title |
|---|
| 刘竹寒、岳秀等: "单级全程自养脱氮工艺研究进展", 《水处理技术》, vol. 43, no. 2, pages 8 - 12 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115043489B (en) | 2024-02-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108483655B (en) | Method for deep denitrification by coupling shortcut nitrification and denitrification with anaerobic ammonia oxidation and sulfur autotrophic denitrification | |
| CN110451641B (en) | Starting method of short-cut denitrification and anaerobic ammonia oxidation coupling denitrification integrated system | |
| CN113415910B (en) | Device and method for denitrification coupling anaerobic ammonium oxidation biological nitrogen and phosphorus removal in iron ammonium oxidation enhanced AAO process | |
| CN112919627B (en) | Method for rapidly starting autotrophic ammonia oxidation by utilizing iron-carbon material | |
| CN112299559B (en) | Whole-process nitrification, short-process denitrification and anaerobic ammonia oxidation single-stage coupling process control method | |
| CN108623012A (en) | A kind of iron ion fortified Anammox denitrification process | |
| EP1805110A1 (en) | Process for the biological denitrification of ammonium containing wastewater | |
| CN111039500A (en) | Short-range and full-range coupled biological denitrification process for treating electroplating wastewater | |
| CN114212884B (en) | Device and method for realizing double short-range coupling anaerobic ammonia oxidation SFBBR deep denitrification of domestic sewage by two-stage water inflow A/O/A | |
| CN106542636B (en) | A kind of method of quick start whole process autotrophic denitrification | |
| CN110683646A (en) | Process for rapidly realizing short-cut nitrification and denitrification of leather wastewater | |
| CN114684925B (en) | Short-cut nitrification treatment method for ammonia-containing wastewater | |
| CN109879428B (en) | Method for realizing short-cut denitrification process of municipal sewage by using delayed anaerobic/low-carbon anoxic SBR | |
| CN116715351A (en) | Based on Fe 2+ And Fe (Fe) 3+ Circularly driven sewage biological denitrification method | |
| CN115385450B (en) | SND-MSAD deep denitrification and carbon removal process by sulfur autotrophic mud method | |
| CN115043489A (en) | Method for enhancing single-stage autotrophic nitrogen removal performance | |
| CN211896290U (en) | Sewage treatment device system | |
| CN115259375A (en) | Device and method for strengthening anaerobic ammonia oxidation and denitrification dephosphorization of AOA process by staged water inflow | |
| CN114230006A (en) | Natural enrichment method for anaerobic ammonium oxidation bacteria | |
| CN211644995U (en) | Non-nitrous excessive accumulation CANON-MBBR system | |
| CN114105287A (en) | Synchronous nitrification and denitrification feed-forward control method for aerobic particle sequencing batch sludge reactor | |
| CN106430576A (en) | Efficient denitrification type anaerobic ammonia oxidation film biological reaction system and method | |
| CN115043488B (en) | Method for regulating and controlling single-stage autotrophic denitrification performance | |
| CN115261261B (en) | Autotrophic ammonia oxidizing bacteria enrichment method | |
| CN116947215B (en) | Multi-process deep denitrification coupling in-situ fermentation dephosphorization device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |