CN220926466U - Double-mud-age composite denitrification reactor based on carbon source recovery - Google Patents
Double-mud-age composite denitrification reactor based on carbon source recovery Download PDFInfo
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- CN220926466U CN220926466U CN202322658414.0U CN202322658414U CN220926466U CN 220926466 U CN220926466 U CN 220926466U CN 202322658414 U CN202322658414 U CN 202322658414U CN 220926466 U CN220926466 U CN 220926466U
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 58
- 239000002131 composite material Substances 0.000 title claims abstract description 25
- 238000011084 recovery Methods 0.000 title claims abstract description 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000005273 aeration Methods 0.000 claims abstract description 32
- 230000003647 oxidation Effects 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 22
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 21
- 238000004062 sedimentation Methods 0.000 claims abstract description 14
- 238000010992 reflux Methods 0.000 claims description 40
- 241000894006 Bacteria Species 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 11
- 238000005276 aerator Methods 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 46
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 23
- 239000010802 sludge Substances 0.000 abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 18
- 230000001651 autotrophic effect Effects 0.000 abstract description 17
- 230000008569 process Effects 0.000 abstract description 16
- 238000005265 energy consumption Methods 0.000 abstract description 15
- 239000010865 sewage Substances 0.000 abstract description 14
- 230000008878 coupling Effects 0.000 abstract description 5
- 238000010168 coupling process Methods 0.000 abstract description 5
- 238000005859 coupling reaction Methods 0.000 abstract description 5
- 238000012258 culturing Methods 0.000 abstract description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 9
- 230000001105 regulatory effect Effects 0.000 description 7
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 230000009935 nitrosation Effects 0.000 description 3
- 238000007034 nitrosation reaction Methods 0.000 description 3
- 235000010288 sodium nitrite Nutrition 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 241001453382 Nitrosomonadales Species 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 238000007885 magnetic separation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- XKLJHFLUAHKGGU-UHFFFAOYSA-N nitrous amide Chemical compound ON=N XKLJHFLUAHKGGU-UHFFFAOYSA-N 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000003403 water pollutant Substances 0.000 description 1
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Abstract
The utility model relates to a double-sludge-age composite denitrification reactor based on carbon source recovery, which comprises an intermediate water tank, an A 2/O reactor, a sedimentation tank and the like, wherein the A 2/O reactor is divided into an anaerobic zone, an anoxic zone and an aerobic zone. The anaerobic ammonia oxidation flora and the conventional flora coexist and a double sludge age composite denitrification system combining long sludge age and short sludge age is formed by culturing the conventional flora and anaerobic ammonia oxidation biomembrane for sewage treatment, and the coupling of whole autotrophic denitrification and heterotrophic denitrification based on anaerobic ammonia oxidation is realized in the same reactor. The carbon source recovery effluent is treated in the system by anaerobic zone heterotrophic denitrification, anoxic zone autotrophic denitrification, aerobic zone nitrification and the like, so that the autotrophic denitrification contribution rate reaches about 22.22%, the carbon source about 20% in the denitrification process and the aeration energy consumption about 12% in the nitrification process are saved, the consumption of the carbon source and the nitrogen source can be reduced, the aeration energy consumption is reduced and the like while the higher effluent quality is ensured, and the system running cost is greatly reduced.
Description
Technical Field
The utility model belongs to the technical field of environmental protection and sewage treatment, and particularly relates to a double-sludge-age composite denitrification reactor based on carbon source recovery.
Background
Because the urban sewage in China has the characteristic of low C/N ratio, the maximum recycling utilization is difficult to realize directly through the anaerobic treatment technology, and the problems can be solved by recycling the carbon source in the urban sewage through the carbon source recycling technologies such as magnetic separation and the like. The municipal sewage after the carbon source recovery treatment still has the characteristic of low C/N ratio, most of sewage treatment plants in China adopt the technology based on the nitrification-denitrification principle to treat the sewage, and the carbon source is added to strengthen denitrification, and high aeration energy consumption is needed to strengthen nitrification reaction, so that the defects of high carbon source consumption, high energy consumption, high sludge yield and the like are overcome.
Autotrophic denitrification based on anaerobic ammonia oxidation is a novel economic and effective denitrification technology, and has the advantages of high denitrification load, no need of carbon source addition, low energy consumption and the like. However, the technology has the bottleneck problems of low ammonia nitrogen concentration, higher carbon source concentration, low temperature and the like in urban sewage treatment application: under the conditions of low ammonia nitrogen concentration and low temperature, anaerobic ammonia oxidation bacteria grow slowly, nitrosation is difficult to regulate and control, so that nitrite oxidation bacteria compete with anaerobic ammonia oxidation bacteria for nitrosamine, and a high carbon source concentration can cause mass propagation and growth of heterotrophic bacteria, compete with anaerobic ammonia oxidation bacteria for matrixes and living spaces, and effluent is difficult to reach a high level and needs further treatment. The utility model combines autotrophic nitrogen removal with traditional nitrification and denitrification heterotrophic nitrogen removal technology, takes advantage of the shortages, and realizes the efficient nitrogen removal of sewage with low carbon source consumption by coupling autotrophic nitrogen removal and heterotrophic nitrogen removal, thereby reducing carbon source consumption, energy consumption and the like.
Disclosure of utility model
In order to solve the problems of high carbon source consumption, high energy consumption, and the like in the existing carbon source recovery sewage treatment technology, the utility model provides the double-sludge-age composite denitrification reactor based on carbon source recovery, which realizes the efficient denitrification of sewage with low carbon source consumption by coupling autotrophic denitrification and heterotrophic denitrification, thereby saving energy consumption, carbon source consumption and the like.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
the double-sludge-age composite denitrification reactor based on carbon source recovery comprises an intermediate water tank, an A 2/O reactor, a sedimentation tank and a central control system, wherein the A 2/O reactor is respectively connected with the intermediate water tank and the sedimentation tank, an anaerobic zone, an anoxic zone and an aerobic zone are arranged in the A 2/O reactor, a partition plate is arranged between the three zones and communicated through a pipeline arranged on the partition plate, a stirrer is arranged in each of the three zones, the anoxic zone is provided with an anoxic aeration system, the aerobic zone is provided with an aerobic aeration system, and anaerobic ammonia oxidizing bacteria biological membrane suspended filler is also added in the anoxic zone;
The sedimentation tank is provided with a slow stirrer and an external reflux system, one end of the external reflux system is connected to the bottom of the sedimentation tank, and the other end of the external reflux system is led into the anaerobic zone;
The stirrer, the anoxic aeration system, the aerobic aeration system, the slow stirrer and the external reflux system are all provided with circuits which are connected to the central control system.
The A 2/O reactor is also provided with an internal reflux system, one end of the internal reflux system is connected to the side edge of the aerobic zone through a pipeline, the other end of the internal reflux system is led into the bottom of the anoxic zone, and the internal reflux system is provided with a circuit connected to the central control system.
The anoxic aeration system is provided with a microporous aerator and an air pump.
The aerobic aeration system is provided with a microporous aerator and a fan.
The anaerobic ammonia oxidation bacteria biomembrane suspending filler is K3 type.
The filling rate of the anaerobic ammonia oxidation bacteria biomembrane filler is 20%.
Compared with the prior art, the double-sludge-age composite denitrification reactor based on carbon source recovery has the following characteristics and beneficial effects:
1. The anaerobic ammonia oxidation flora and the conventional flora coexist and a double sludge age composite denitrification system combining long sludge age and short sludge age is formed by culturing the conventional flora and the anaerobic ammonia oxidation biomembrane in the same reactor, and the coupling of whole autotrophic denitrification and heterotrophic denitrification based on anaerobic ammonia oxidation is realized in the same reactor. Compared with the prior art, the system can save about 20% of carbon source in the denitrification process without adding any additional carbon source when in operation, and can save about 12% of aeration energy consumption in the nitrification process, so that the system can reduce the carbon source consumption and the energy consumption while ensuring higher effluent quality;
2. The denitrification effect without adding the nitrogen source in the utility model has little difference with the denitrification effect with adding the nitrogen source in the prior art, so the utility model can save the nitrogen source compared with the prior art;
3. In the utility model, autotrophic denitrification and heterotrophic denitrification are combined, and the autotrophic denitrification contribution rate is more than 20%.
Drawings
FIG. 1 is a schematic diagram of a double-sludge-age composite denitrification reactor based on carbon source recovery according to an embodiment of the utility model;
FIG. 2 is a flow chart of a double sludge age composite denitrification method based on carbon source recovery according to an embodiment of the utility model.
Detailed Description
Embodiments of the present utility model will be described in detail below with reference to the accompanying drawings and examples.
In order to solve the problems of high energy consumption, high carbon source consumption and the like of the existing carbon source recovery sewage treatment technology, the double-sludge-age composite denitrification reactor based on carbon source recovery realizes the coupling of whole-course autotrophic denitrification and heterotrophic denitrification based on anaerobic ammonia oxidation in the same reactor, and achieves the purposes of high-efficiency denitrification, energy consumption and carbon source consumption conservation of sewage with low carbon source consumption.
As shown in figure 1, the double-sludge-age composite denitrification reactor based on carbon source recovery comprises an intermediate water tank 1, an A 2/O reactor 2, a sedimentation tank 3 and a central control system 4, wherein the A 2/O reactor 2 is respectively connected with the intermediate water tank 1 and the sedimentation tank 3, water in the intermediate water tank 1 is pumped into the reactor through a water inlet pump 1.1, an anaerobic zone a, an anoxic zone b and an aerobic zone c are arranged in the A 2/O reactor, a partition plate 2.1 is arranged between the three zones and communicated through a pipeline arranged on the partition plate 2.1, a stirrer 2.2 is arranged in each of the three zones, an anoxic aeration system is arranged in the anoxic zone b, an aerobic aeration system is arranged in the aerobic zone c, and anaerobic ammonia oxidation bacteria biofilm suspended filler 2.6 is also added in the anoxic zone b;
The sedimentation tank 3 is provided with a slow stirrer 3.1 and an external reflux system, one end of the external reflux system is connected to the bottom of the sedimentation tank 3, the other end of the external reflux system is led into the anaerobic zone a, and the sedimentation sludge at the bottom of the sedimentation tank 3 is refluxed to the anaerobic zone a through an external reflux pump 3.2.
The A 2/O reactor is also provided with an internal reflux system, one end of the internal reflux system is connected to the side edge of the aerobic zone c through a pipeline, the other end of the internal reflux system is introduced into the bottom of the anoxic zone b, and sludge in the aerobic zone c is refluxed to the anoxic zone b through an internal reflux pump 2.7.
The anoxic aeration system is provided with a microporous aerator 2.3 and an air pump 2.5.
The aerobic aeration system is provided with a microporous aerator 2.3 and a fan 2.4.
The anaerobic ammonia oxidation bacteria biomembrane suspending filler 2.6 can be K3 type, and the filling rate is about 20%.
The water inlet pump 1.1, the stirrer 2.2, the fan 2.4, the air pump 2.5, the internal reflux pump 2.7, the slow stirrer 3.1 and the external reflux pump 3.2 are all provided with circuits which are connected to the central control system 4.
The central control system 4 adjusts the stirrer 2.2 through the frequency converter to ensure that the suspended sludge and the suspended filler in the reactor are in a good mixing state, and the central control system 4 adjusts the rotating speed of the slow stirrer 3.1 through the frequency converter to prevent the dead sludge; the working frequency of the fan 2.4 and the air pump 2.5 can be adjusted through the frequency converter, so that the precise control of the aeration amount of the reactor is realized; the shaft power of the water inlet pump 1.1, the internal reflux pump 2.7 and the external reflux pump 3.2 can be adjusted through the frequency converter, so that the accurate control of the water inlet flow and the internal and external reflux amounts is realized.
As shown in FIG. 2, the double-sludge-age composite denitrification method based on carbon source recovery comprises the following steps:
Step one, starting an A 2/O process: inoculating sludge in the reactor to start an A 2/O reactor, and performing aeration activation for about 3 days after sludge inoculation to form a heterotrophic denitrification region of suspended sludge (short sludge age);
Step two, enriching anaerobic ammonia oxidizing bacteria: inoculating a suspended filler 2.6 attached with an anaerobic ammonia oxidation bacterial biomembrane in the anoxic zone b, and adding sodium nitrite to recover and strengthen the activity of the anaerobic ammonia oxidation biomembrane, wherein the concentration of the fed sodium nitrite is from low to high, the concentration is between 2 mg/L and 10mg/L, the filler filling rate is about 20 percent, and after the anoxic zone b forms a biomembrane (long sludge age) autotrophic denitrification zone, a double sludge age composite denitrification system of the suspended sludge (short sludge age) heterotrophic denitrification zone and the biomembrane (long sludge age) autotrophic denitrification zone is formed in the reactor;
Regulating and controlling micro-oxygen nitrosation: stopping adding sodium nitrite after the formation of the double-sludge-age composite denitrification system, starting an inner reflux system and an outer reflux system through a central control system 4, adopting aerobic/anoxic intermittent aeration in an anoxic zone b, wherein the aeration time is 5-20min, preferably 15min, starting an anoxic aeration system through the central control system during aerobic aeration to control the concentration of dissolved oxygen to be 0.1-0.3mg/L, and closing the anoxic aeration system during anoxic aeration;
Fourth, regulating and controlling an internal and external reflux system: the internal and external reflux ratio of the internal and external reflux systems is regulated by the central control system 4, so that the internal reflux ratio is gradually regulated to 0% from 0% -150%, the ammonia nitrogen concentration of the inlet water of the anoxic zone is further improved, the autotrophic denitrification process is enhanced, during the period, the ammonia nitrogen concentration of the inlet water and the outlet water is measured, the reduction of the internal reflux amount is ensured not to significantly influence the denitrification effect of the reactor, and the internal reflux system is finally closed; the external reflux ratio was controlled to 100%.
When the reactor stably runs, the central control system 4 regulates and controls the anoxic aeration system to maintain intermittent aeration of the anoxic zone b, the external reflux ratio of the external reflux system is regulated to be 100%, the aerobic aeration system is regulated and controlled to maintain the dissolved oxygen concentration of the aerobic zone c at 1-3mg/L, after the sewage is subjected to double-sludge-age composite denitrification and the nitrification treatment of the aerobic zone c, the ammonia nitrogen in the effluent is less than or equal to 2mg/L, the total nitrogen is less than or equal to 10mg/L, and the effluent quality is stable.
In the examples, the reactor 2 has a size of 3.60m long, 1.20m wide, 2.00m high, a volume of 8.64m 3 and an effective volume of 7.80m 3; the length, width and height of the sedimentation tank 3 can be selected to be 1.20m, 1.20m and 1.80m, and the overflow height can be set to be 1.60m; intermittent aeration with 15min aerobic/15 min anoxic conditions is selected; the ambient temperature is 18-22 ℃.
Wherein the average ammonia nitrogen and total nitrogen concentration of the effluent in the first step are respectively 2.60+/-4.30 mg/L and 11.60+/-3.80 mg/L, and the average ammonia nitrogen and total nitrogen removal rates are respectively 87.80% and 47.90%; the average ammonia nitrogen of the effluent in the second step is 0.71mg/L, the average total inorganic nitrogen concentration of the effluent is 7.19+/-1.47 mg/L, and the average removal rates of ammonia nitrogen and total nitrogen are 94.11% and 71.47% respectively; in the third step, the average ammonia nitrogen output of the reactor is 1.00mg/L, the total nitrogen is 8.84mg/L, and the ammonia nitrogen removal rate and the total nitrogen removal rate are 97.00% and 74.00% respectively. It can be seen that the water quality of the effluent in the first step does not meet the A-level standard of the discharge Standard of pollutants of Water treatment plant of urban wastewater treatment plant (DB 11/890-2012) in Beijing, and the water quality of the effluent in the second and third steps can meet the above standard. Because the first step is equivalent to the quality of the effluent when no carbon source is added in the traditional A 2/O process, the effluent can be discharged after reaching the standard by adding the carbon source in engineering; step two, which is equivalent to the traditional anaerobic ammonia oxidation process, a nitrogen source is required to be continuously added to ensure the water quality of the effluent, and the water quality of the effluent is easily influenced by the concentration of ammonia nitrogen and the like of the inlet water; in the third step, the double-sludge composite denitrification process does not need to add a carbon source and a nitrogen source, which means that the system does not need to add the carbon source and the nitrogen source after micro-oxygen nitrosation is regulated and controlled.
According to calculation, the autotrophic nitrogen removal contribution rate reaches about 22.22%, and meanwhile, about 20% of carbon source in the denitrification process and about 12% of aeration energy consumption in the nitrification process can be saved.
In addition, through comparative researches, the concentration of total nitrogen in effluent is 11.6+/-3.8 mg/L when the carbon source is not added in the process of recycling effluent (C/N < 3) by treating the carbon source by the traditional A 2/O technology, and the A-level standard of the discharge Standard of pollutants in urban wastewater treatment plants (DB 11/890-2012) in Beijing city cannot be met, and in order to meet the standard, about 70mg/L of carbon source is required to be additionally added in order to ensure that the total nitrogen concentration in the effluent is about 9mg/L based on 108mg/L of the carbon source of the inlet water. When the same carbon source recovery effluent is treated (C/N is less than 3), the total nitrogen of the effluent is lower than the A-level standard limit value of the discharge Standard of Water pollutants of urban wastewater treatment plants (DB 11/890-2012) in Beijing, and the quality of the effluent is stable. Therefore, it is considered that the utility model saves about 65% of carbon source compared with the traditional A 2/O process when the same carbon source recovery effluent is treated (C/N < 3).
The double-sludge-age composite denitrification reactor based on carbon source recovery realizes the complementary advantages of autotrophic denitrification and heterotrophic denitrification in the same reactor, thereby reducing the carbon source consumption and the energy consumption, the autotrophic denitrification contribution rate is more than 20%, and the carbon source of about 20% in the denitrification process and the aeration energy consumption of about 12% in the nitrification process are saved; even about 65% of carbon source can be saved in the comparison study.
It will be apparent to those skilled in the art from this disclosure that numerous changes and modifications can be made to the reactor and process of the utility model described herein, and such changes and modifications are intended to be included within the scope of the utility model.
Claims (6)
1. A double mud age composite denitrification reactor based on carbon source recovery is characterized in that: the anaerobic ammonia oxidation bacteria biological membrane suspended filler (2.6) is further added in the anoxic zone (b);
The sedimentation tank (3) is provided with a slow stirrer (3.1) and an external reflux system, one end of the external reflux system is connected to the bottom of the sedimentation tank (3), and the other end of the external reflux system is communicated with the anaerobic zone (a);
The stirrer (2.2), the anoxic aeration system, the aerobic aeration system, the slow stirrer (3.1) and the external reflux system are all provided with circuits which are connected to the central control system (4).
2. The double-sludge-age composite denitrification reactor based on carbon source recovery according to claim 1, wherein: the A 2/O reactor is also provided with an internal reflux system, one end of the internal reflux system is connected to the side edge of the aerobic zone (c) through a pipeline, the other end of the internal reflux system is introduced into the bottom of the anoxic zone (b), and the internal reflux system is provided with a circuit connected to the central control system (4).
3. The double-sludge-age composite denitrification reactor based on carbon source recovery according to claim 1, wherein: the anoxic aeration system is provided with a microporous aerator (2.3) and an air pump (2.5).
4. The double-sludge-age composite denitrification reactor based on carbon source recovery according to claim 1, wherein: the aerobic aeration system is provided with a microporous aerator (2.3) and a fan (2.4).
5. The double-sludge-age composite denitrification reactor based on carbon source recovery according to claim 1, wherein: the anaerobic ammonia oxidation bacteria biological film suspending filler (2.6) is K3 type.
6. The double-sludge-age composite denitrification reactor based on carbon source recovery according to claim 1, wherein: the filling rate of the anaerobic ammonia oxidation bacteria biological film suspended filler is 20%.
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