CN109319929B - Integral anaerobic ammonia oxidation reaction system - Google Patents
Integral anaerobic ammonia oxidation reaction system Download PDFInfo
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- CN109319929B CN109319929B CN201811536682.2A CN201811536682A CN109319929B CN 109319929 B CN109319929 B CN 109319929B CN 201811536682 A CN201811536682 A CN 201811536682A CN 109319929 B CN109319929 B CN 109319929B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 30
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 92
- 239000002253 acid Substances 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 238000005273 aeration Methods 0.000 claims abstract description 29
- 238000012544 monitoring process Methods 0.000 claims abstract description 22
- 239000010802 sludge Substances 0.000 claims abstract description 16
- 238000007664 blowing Methods 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 11
- 239000000523 sample Substances 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 15
- 239000010865 sewage Substances 0.000 claims description 15
- 230000000694 effects Effects 0.000 claims description 10
- 230000001174 ascending effect Effects 0.000 claims description 8
- 239000011229 interlayer Substances 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 2
- 241001148470 aerobic bacillus Species 0.000 abstract description 6
- 241001148471 unidentified anaerobic bacterium Species 0.000 abstract description 6
- 230000001580 bacterial effect Effects 0.000 abstract description 5
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000003647 oxidation Effects 0.000 description 14
- 230000006872 improvement Effects 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 241001453382 Nitrosomonadales Species 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
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000011499 joint compound Substances 0.000 description 2
- 238000007034 nitrosation reaction Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
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
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (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)
Abstract
The invention relates to an integrated anaerobic ammonia oxidation reaction system, which comprises a reactor, wherein a water distribution device is arranged at the bottom of the reactor, a support frame is arranged at the top of the reactor, a guide cylinder is arranged above the water distribution device, an aeration pipe is arranged in the guide cylinder, a first baffle plate and a second baffle plate are sequentially arranged above the guide cylinder, the first baffle plate and the second baffle plate are arranged on the support frame at intervals up and down, the first baffle plate is provided with a water through hole, a three-phase separator for separating mud from water and gas is arranged above the second baffle plate, the three-phase separator is arranged on the support frame, and a water outlet and an air outlet are arranged above the three-phase separator; the water inlet tank is connected with the water distribution device; an acid liquid supply device for supplying acid liquid into the reactor; the air blowing device is connected with the aeration pipe; the pH on-line monitoring unit is used for detecting the pH value in the reactor; the DO on-line monitoring unit is used for detecting the DO value in the reactor, and has the advantages of being beneficial to forming granular sludge with larger particle size and aerobic bacteria wrapping anaerobic bacteria and good in bacterial settlement performance.
Description
Technical Field
The invention relates to a sewage treatment technology, in particular to an integrated anaerobic ammonia oxidation reaction system.
Background
The high ammonia nitrogen wastewater in the field of sewage treatment is always a technical problem, and particularly the high ammonia nitrogen wastewater with low carbon nitrogen ratio has higher treatment difficulty. The core of the sewage treatment process is generally a biochemical part, the sewage with serious unbalance of C/N is treated by adopting the traditional biological nitrification and denitrification technology, denitrification cannot be effectively carried out without adding an organic carbon source, and aiming at the limitation, a novel denitrification mechanism and denitrification process, namely an anaerobic ammonia oxidation process, are developed in recent years. The anaerobic ammonia oxidation process has irreplaceable superiority for treating low C/N wastewater because of the advantages of no need of additional organic carbon source, high denitrification load, low running cost, small occupied space and the like, and researches and developments of sewage treatment processes taking anaerobic ammonia oxidation as a main body bring the problems of difficult denitrification, high energy consumption, large sludge yield and the like of low carbon-nitrogen ratio wastewater facing the current sewage treatment industry in China.
However, the anaerobic ammonia oxidation strain has long generation period, slow growth, severe growth environment conditions, high oxygen concentration and excessive concentration of ammonium salt and nitrite matrixes can inhibit the activity of the strain, so that the anaerobic ammonia oxidation reactor is slow to start, and pure culture is difficult to realize.
The anaerobic ammoxidation process may be divided into an integrated and a two-stage process. The integrated process has the advantages of lower capital cost, smaller occupied area, easier operation and capability of avoiding nitrite inhibition. However, the traditional integrated process has long starting time, complex ecological relationship among microorganisms in the reactor, easy instability when being subjected to load impact, and difficult control of optimal conditions to enable shortcut nitrification and anaerobic ammonia oxidation to be carried out in the same reactor.
The two reactors in the two-stage process can be independently and flexibly and stably regulated and controlled, the recovery time of the system after being disturbed is short, and the inflow water of the ANAMMOX reactor has relatively stable proportion of ammonia nitrogen and nitrite nitrogen. However, the investment cost of the two-stage process is high, and when the treatment capacity is improved, the return flow can only be increased to dilute the front-end water inflow, so that nitrite in the reactor is easy to accumulate.
At present, a conventional anaerobic ammonia oxidation SBR reactor cannot continuously feed water, the concentration of a substrate, the temperature, the pH and DO (dissolved oxygen) in the reactor fluctuate greatly, and a large enough hydraulic ascending flow rate cannot be provided, so that granular sludge is difficult to form; when the concentration of nitrite nitrogen in the water is higher, the one-time water inlet mode can inhibit the anaerobic ammoxidation reaction, so that the reaction rate of the anaerobic ammoxidation is reduced; granular sludge is easily crushed into flocculent sludge in the stirring process of the reactor, so that bacterial settlement performance is poor, bacterial loss is serious during drainage, anaerobic ammonia oxidation bacteria are difficult to effectively stay in the reactor, and the starting time of an anaerobic ammonia oxidation process is long.
Disclosure of Invention
The invention aims to solve the technical problems of overcoming the defects of the prior art and providing an integrated anaerobic ammonia oxidation reaction system which is favorable for forming granular sludge with larger particle size and anaerobic bacteria wrapped by aerobic bacteria and has good bacterial settlement performance.
In order to solve the technical problems, the invention adopts the following technical scheme:
an integrated anaerobic ammonia oxidation reaction system comprising:
The reactor comprises a reactor, wherein a water distribution device is arranged at the bottom in the reactor, a support frame is arranged at the top of the reactor, a guide cylinder is arranged above the water distribution device, an aeration pipe is arranged in the guide cylinder, a first baffle plate and a second baffle plate are sequentially arranged above the guide cylinder, the first baffle plate and the second baffle plate are arranged on the support frame at intervals up and down, the first baffle plate is provided with water through holes, a three-phase separator for separating mud, water and gas is arranged above the second baffle plate, the three-phase separator is arranged on the support frame, and a water outlet and an air outlet are arranged above the three-phase separator;
The water inlet tank is connected with the water distribution device;
An acid liquid supply device for supplying acid liquid into the reactor;
the air blowing device is connected with the aeration pipe;
the pH on-line monitoring unit is used for detecting the pH value in the reactor;
And the DO online monitoring unit is used for detecting the DO value in the reactor.
As a further improvement of the above technical solution, preferably, the diameter of both ends of the guide cylinder is larger than the diameter of the middle part, and the diameter of the upper end is larger than the diameter of the lower end.
As a further improvement of the above technical solution, preferably, the second baffle is an umbrella-shaped baffle.
As a further improvement of the above technical solution, preferably, the first baffle is a circular baffle.
As a further improvement of the technical scheme, preferably, the water inlet tank is connected with the water distribution device through a water inlet pipe, and a water inlet pump is arranged on the water inlet pipe.
As a further improvement of the technical scheme, preferably, the water outlet is provided with a water outlet pipe, the water outlet pipe is provided with an overflow groove, the water outlet pipe is divided into two branches, one branch is a water outlet branch, the other branch is a circulating water inlet branch, and the circulating water inlet branch is connected with the water inlet tank.
As a further improvement of the above technical scheme, preferably, the aeration pipe is circumferentially provided with uniformly distributed aeration guide holes.
As a further improvement of the technical scheme, preferably, the acid liquid supply device comprises an acid liquid tank, the acid liquid tank is connected with the reactor through an acid inlet pipe, an acid inlet pump is arranged on the acid inlet pipe, the pH on-line monitoring unit comprises a pH on-line monitor and a pH probe, the pH probe is positioned in the reactor, and the pH on-line monitor is connected with the acid inlet pump.
As a further improvement of the above technical solution, preferably, the air blowing device includes a blower connected to the aeration pipe through an air inlet pipe, and the DO on-line monitoring unit includes a DO on-line monitor and a DO probe, the DO probe is located in the reactor, and the DO on-line monitor is connected to the blower.
As a further improvement of the above technical scheme, preferably, an outer wall of the reactor is provided with a heat-insulating interlayer.
Compared with the prior art, the invention has the advantages that:
the invention aims to provide an integrated anaerobic ammonia oxidation reactor, which can provide enough hydraulic ascending flow rate for the reactor through the guide aeration of an aeration pipe in a guide cylinder, thereby being beneficial to the formation of sludge particles with large particle size; the baffling effect of the first baffle plate and the second baffle plate greatly enhances the internal circulation of the reactor, the concentration of the matrix in the reactor is more uniform, and the temperature, the pH and the DO are more stable; the internal circulation replaces the traditional stirring mode, so that the damage of mechanical shearing force generated by stirring to the granular sludge can be reduced to the greatest extent, the aerobic bacteria can wrap anaerobic bacteria to form granular sludge better, the granular sludge with larger particle size and with the anaerobic bacteria wrapped by the aerobic bacteria can be formed, and good coexistence of the aerobic ammonia oxidizing bacteria and the anaerobic ammonia oxidizing bacteria in one reactor is realized; under the baffling effect of the first baffle and the second baffle, the rising flow rate of the solution is slowed down, the sedimentation performance of large-particle sludge formed in the reactor is good, the sludge and water can be effectively separated after passing through the three-phase separator, the strain is not easy to run off, and the starting of the reactor is accelerated.
Drawings
Fig. 1 is a schematic structural view of the present invention.
FIG. 2 is a schematic view of the structure of an aerator pipe according to the invention.
Fig. 3 is a schematic diagram of the operation of the present invention.
The reference numerals in the drawings denote:
1. A water inlet tank; 11. a water inlet pipe; 12. a water inlet pump; 2. a reactor; 21. a water distribution device; 22. a support frame; 23. a guide cylinder; 24. an aeration pipe; 241. aeration guide holes; 25. a first baffle; 251. a water through hole; 26. a second baffle; 27. a three-phase separator; 28. a water outlet; 29. an exhaust port; 3. an acid liquid supply device; 31. an acid liquor tank; 32. an acid inlet pipe; 33. an acid feeding pump; 4. an air blowing device; 41. a blower; 42. an air inlet pipe; 5. a pH on-line monitoring unit; 51. a pH on-line monitor; 52. a pH probe; 6. DO on-line monitoring unit; 61. DO on-line monitor; 62. a DO probe; 7. a drain pipe; 71. a drainage branch; 72. a circulating water inlet branch; 8. an overflow trough; 9. and (5) heat preservation interlayer.
Detailed Description
The invention is described in further detail below with reference to the drawings and specific examples of the specification.
As shown in fig. 1 to 3, the integrated anaerobic ammonia oxidation reaction system of the present embodiment includes a reactor 2, a water inlet tank 1, an acid liquid supply device 3, a blowing device 4, a pH on-line monitoring unit 5, and a DO on-line monitoring unit 6.
Wherein, the bottom in the reactor 2 is equipped with water distribution device 21, the top is equipped with support frame 22, the top of water distribution device 21 is equipped with guide cylinder 23, guide cylinder 23 both ends all communicate with the inside of reactor 2, be equipped with aeration pipe 24 in the guide cylinder 23, guide cylinder 23 top is equipped with first baffle 25 and second baffle 26 in proper order, first baffle 25 and second baffle 26 are installed on support frame 22 with the interval from top to bottom, first baffle 25 is located the below of second baffle 26, first baffle 25 is equipped with limbers 251, the water of below of being convenient for passes, the top of second baffle 26 is equipped with the three-phase separator 27 of separation mud water gas, three-phase separator 27 installs on support frame 22, reactor 2 is equipped with outlet 28 and gas vent 29 in the top of three-phase separator 27. The water inlet tank 1 is connected with the water distribution device 21 and is used for providing sewage into the reactor 2, the acid liquid supply device 3 is used for providing acid liquid into the reactor 2 so as to adjust the pH value, the air blowing device 4 is connected with the aeration pipe 24 and blows air into the guide cylinder 23, the pH on-line monitoring unit 5 is used for detecting the pH value in the reactor 2, and the DO on-line monitoring unit 6 is used for detecting the DO (dissolved oxygen) value in the reactor 2.
The guide cylinder 23 is provided with anaerobic bacteria, and aerobic bacteria are arranged outside the guide cylinder 23 and are respectively used for treating sewage. As shown in fig. 3, when the reactor 2 is operating normally, sewage enters the water distribution device 21 in the water inlet tank 1, and is uniformly injected into the guide cylinder 23 by the water distribution device 21. Six uniformly arranged aeration pipes 24 are arranged in the middle of the guide cylinder 23, when the aeration pipes 24 are used for aeration, air is jetted upwards to provide enough hydraulic ascending flow velocity, solution is taken to pass through the guide cylinder 23 upwards, the first baffle 25 above the guide cylinder 23 deflects down the two sides above the guide cylinder 23 through the solution, the second baffle 26 deflects down the solution passing through the middle of the guide cylinder 23, the baffling down solution also has the scouring effect on the first baffle 25, the bacterial accumulation on the first baffle 25 is avoided, the common baffling effect of the first baffle 25 and the second baffle 26 can lead the solution to be gently split and then baffle downwards, the large area of the solution cannot be returned into the guide cylinder 23 due to the interception of the baffles, and the phenomenon of the liquid flow direction in the reactor 2 is disturbed (if a baffle is directly arranged above the guide cylinder 23, the phenomenon can be caused). The solution which is deflected downwards enters the guide cylinder 23 again from the bottom of the guide cylinder 23, and the internal circulation process is completed, and the flow directions of gas and liquid during the internal circulation are respectively shown by a dotted line and a solid line in fig. 3. The first baffle 25 and the second baffle 26 have baffling effect, the hydraulic ascending flow rate of the solution is slowed down, the mud, water and gas three phases are fully separated through the three-phase separator 27, the gas is discharged from the gas outlet 29 of the reactor 2, the treated liquid is discharged from the gas outlet 28, the reactor 2 is internally provided with the pH on-line monitoring unit 5 and the DO on-line monitoring unit 6, and when the pH value is higher than the set range, the acid liquid is supplied to the reactor 2 by the acid liquid supply device 3 until the pH value is reduced to the set range; when the DO value is higher than the set range, the air blowing means 4 reduces the air intake amount until the DO value falls to the set range, thus maintaining the DO value in the reactor 2 within a constant range.
In this embodiment, the diameter of the two ends of the guide cylinder 23 is larger than that of the middle part, the diameter of the upper end is larger than that of the lower end, the middle is narrow, the rising flow rate of water conservancy is increased, the liquid can quickly pass through the guide cylinder 23, an upward flow direction is formed, and the upper head width is used for slowing down the flow rate, and the strain sedimentation and the baffling of the two baffles are facilitated.
In this embodiment, the support 22 is a support rod, and the second baffle 26 is an umbrella-shaped baffle, which is fixed on the support rod. The first baffle 25 is a circular baffle, and is fixed on the support rod by four support beams.
In this embodiment, the water inlet tank 1 is connected to the water distribution device 21 through a water inlet pipe 11, and a water inlet pump 12 is disposed on the water inlet pipe 11. The sewage in the water inlet tank 1 is pumped into the reactor 2 by the water inlet pump 12.
In this embodiment, the drain port 28 is provided with a drain pipe 7, the drain pipe 7 is provided with an overflow groove 8, the drain pipe 7 is divided into two branches, one branch is a drain branch 71, the other branch is a circulating water inlet branch 72, and the circulating water inlet branch 72 is connected with the water inlet tank 1 to regulate the concentration of sewage in the water inlet tank 1. The treated sewage is overflowed and discharged through the overflow groove 8, a part of the sewage is discharged, and the other part of the sewage can flow back to the water inlet tank 1, and mud is settled and flows back.
In this embodiment, aeration guide holes 241 are uniformly distributed in the circumferential direction of the aeration pipe 24, and under the action of the guide holes, aeration can provide a larger upward hydraulic ascending flow rate.
In this embodiment, the acid liquid supply device 3 includes an acid liquid tank 31, the acid liquid tank 31 is connected with the reactor 2 through an acid inlet pipe 32, an acid inlet pump 33 is arranged on the acid inlet pipe 32, the pH on-line monitoring unit 5 includes a pH on-line monitor 51 and a pH probe 52, the pH probe 52 is located in the reactor 2, and the pH on-line monitor 51 is in control connection with the acid inlet pump 33.
The blowing device 4 comprises a blower 41, the blower 41 is connected with the aeration pipe 24 through an air inlet pipe 42, the DO online monitoring unit 6 comprises a DO online monitor 61 and a DO probe 62, the DO probe 62 is positioned in the reactor 2, and the DO online monitor 61 is in control connection with the blower 41.
When the pH probe 52 detects that the pH value of the solution in the reactor 2 is higher than the set range, the pH on-line monitor 51 controls the acid feeding pump 33 to be started until the pH value is reduced to the set range, and the acid feeding pump 33 stops working; when the DO probe 62 detects that the DO value of the solution in the reactor 2 is higher than the set range, the DO on-line monitor 61 decreases the air intake of the blower 41 until the DO value falls to the set range, thus keeping the DO value in the reactor 2 within a constant range.
In the embodiment, the outer wall of the reactor 2 is provided with a heat-insulating interlayer 9, and the temperature of heat-insulating water in the interlayer is controlled by an external circulation heat-insulating temperature control system.
According to the integrated anaerobic ammonia oxidation reaction system, DO value in the guide cylinder 23 is slightly higher than that of the guide cylinder 23, nitrosation reaction of strains in the guide cylinder 23 is slightly stronger than that of anaerobic ammonia oxidation reaction, and aerobic bacteria gradually wrap anaerobic bacteria. However, due to the internal circulation effect, the solution rapidly passes through the guide cylinder 23, and the anaerobic ammonia oxidation reaction outside the guide cylinder 23 is slightly stronger than the nitrosation reaction, so that good coexistence of aerobic ammonia oxidation bacteria and anaerobic ammonia oxidation bacteria in one reactor 2 is realized. When the reactor 2 is started, if the strain in the reactor 2 is flocculent sludge or granular sludge with smaller particle size, activated carbon can be properly added as an adsorption carrier to accelerate the formation of granular sludge with large particle size.
Comparative example: when the conventional reactor is started, optimal conditions are difficult to control so that shortcut nitrification and anaerobic ammonia oxidation are performed in the same reactor, the reactor is easy to be impacted, the activity of strains is easy to be inhibited, if no anaerobic ammonia oxidation strain with good activity and larger particle size is used as seed mud, the conventional reactor generally needs 6-8 months to start.
This embodiment: with the reactor 2 of this embodiment, the start-up period of the reactor 2 is generally 4 months, and the start-up period of the reactor 2 is shortened by 33% -50%.
While the invention has been described with reference to preferred embodiments, it is not intended to be limiting. Many possible variations and modifications of the disclosed technology can be made by anyone skilled in the art, or equivalent embodiments with equivalent variations can be made, without departing from the scope of the invention. Therefore, any simple modification, equivalent variation and modification of the above embodiments according to the technical substance of the present invention shall fall within the scope of the technical solution of the present invention.
Claims (6)
1. An integrated anaerobic ammonia oxidation reaction system, comprising:
The reactor comprises a reactor (2), wherein a water distribution device (21) is arranged at the bottom in the reactor (2), a supporting frame (22) is arranged at the top of the reactor, a guide cylinder (23) is arranged above the water distribution device (21), the diameters of the two ends of the guide cylinder (23) are larger than those of the middle part, the diameters of the upper ends of the guide cylinder are larger than those of the lower ends of the guide cylinder, an aeration pipe (24) is arranged in the guide cylinder (23), a first baffle (25) and a second baffle (26) are sequentially arranged above the guide cylinder (23), the first baffle (25) and the second baffle (26) are arranged on the supporting frame (22) at intervals up and down, a water through hole (251) is formed in the first baffle (25), a three-phase separator (27) for separating mud and water is arranged above the second baffle (26), the three-phase separator (27) is arranged on the supporting frame (22), and a water outlet (28) and a water outlet (29) are arranged above the three-phase separator (27); aeration guide holes (241) are uniformly distributed in the circumferential direction of the aeration pipe (24), and under the action of the guide holes, aeration can provide larger upward hydraulic ascending flow rate, so that sludge particles with large particle size are formed; the first baffle (25) is a circular baffle; the second baffle (26) is an umbrella-shaped baffle;
The water inlet tank (1), the water inlet tank (1) is connected with the water distribution device (21);
An acid liquid supply device (3), wherein the acid liquid supply device (3) is used for supplying acid liquid into the reactor (2);
the air blowing device (4), the said air blowing device (4) is connected with aeration pipe (24);
The pH on-line monitoring unit (5) is used for detecting the pH value in the reactor (2);
a DO on-line monitoring unit (6) for detecting DO values in the reactor (2);
When the reactor (2) is in normal operation, sewage enters the water distribution device (21) from the water inlet tank (1), and is uniformly injected into the guide cylinder (23) through the water distribution device (21); an aeration pipe (24) is arranged in the middle of the guide cylinder (23), when the aeration pipe (24) is used for aeration, air is jetted upwards to provide enough hydraulic ascending flow rate, the solution is taken to pass through the guide cylinder (23) upwards, the first baffle (25) above the guide cylinder (23) deflects down the two sides above the guide cylinder (23) through the solution, the second baffle (26) deflects down the solution passing through the middle of the guide cylinder (23), the downward solution is deflected down the first baffle (25), the first baffle (25) is prevented from accumulating strains, the first baffle (25) and the second baffle (26) have common deflection, the solution can be gently split and then deflected downwards, and the large-area back mixing in the guide cylinder (23) can not be caused by the interception of the baffles, so that the flow direction of the liquid in the reactor (2) is disturbed; the solution which is deflected downwards enters the guide cylinder (23) again from the bottom of the guide cylinder (23) to finish the internal circulation process; the first baffle (25) and the second baffle (26) have baffling effect, the hydraulic ascending flow rate of the solution is slowed down, the mud, water and gas are fully separated through the three-phase separator (27), the gas is discharged from the gas outlet (29) of the reactor (2), and the treated liquid is discharged from the water outlet (28); the reactor (2) is internally provided with a pH on-line monitoring unit (5) and a DO on-line monitoring unit (6), when the pH value is higher than a set range, the acid liquid supply device (3) supplies acid liquid into the reactor (2) until the pH value is reduced to the set range; when the DO value is higher than the set range, the air blowing device (4) reduces the air inlet amount until the DO value is reduced to the set range, so that the DO value in the reactor (2) is kept within a constant range.
2. The integrated anaerobic ammonia oxidation reaction system according to claim 1, wherein the water inlet tank (1) is connected with the water distribution device (21) through a water inlet pipe (11), and a water inlet pump (12) is arranged on the water inlet pipe (11).
3. The integrated anaerobic ammonia oxidation reaction system according to claim 1, wherein the water outlet (28) is provided with a water outlet pipe (7), an overflow groove (8) is arranged on the water outlet pipe (7), the water outlet pipe (7) is divided into two branches, one branch is a water outlet branch (71), the other branch is a circulating water inlet branch (72), and the circulating water inlet branch (72) is connected with the water inlet tank (1).
4. The integrated anaerobic ammonia oxidation reaction system according to claim 1, wherein the acid liquid supply device (3) comprises an acid liquid tank (31), the acid liquid tank (31) is connected with the reactor (2) through an acid inlet pipe (32), an acid inlet pump (33) is arranged on the acid inlet pipe (32), the pH online monitoring unit (5) comprises a pH online monitor (51) and a pH probe (52), the pH probe (52) is positioned in the reactor (2), and the pH online monitor (51) is connected with the acid inlet pump (33).
5. The integrated anaerobic ammonia oxidation reaction system according to claim 1, wherein the blowing device (4) comprises a blower (41), the blower (41) is connected with the aeration pipe (24) through an air inlet pipe (42), the DO on-line monitoring unit (6) comprises a DO on-line monitor (61) and a DO probe (62), the DO probe (62) is located in the reactor (2), and the DO on-line monitor (61) is connected with the blower (41).
6. The integrated anaerobic ammonia oxidation reaction system according to claim 1, wherein the outer wall of the reactor (2) is provided with a heat-insulating interlayer (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811536682.2A CN109319929B (en) | 2018-12-14 | 2018-12-14 | Integral anaerobic ammonia oxidation reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811536682.2A CN109319929B (en) | 2018-12-14 | 2018-12-14 | Integral anaerobic ammonia oxidation reaction system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109319929A CN109319929A (en) | 2019-02-12 |
| CN109319929B true CN109319929B (en) | 2024-06-18 |
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