CN105502664A - Device using AB-ASBR reactors to start anaerobic ammonia oxidation - Google Patents
Device using AB-ASBR reactors to start anaerobic ammonia oxidation Download PDFInfo
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- CN105502664A CN105502664A CN201610102527.4A CN201610102527A CN105502664A CN 105502664 A CN105502664 A CN 105502664A CN 201610102527 A CN201610102527 A CN 201610102527A CN 105502664 A CN105502664 A CN 105502664A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title abstract description 8
- 229910021529 ammonia Inorganic materials 0.000 title abstract description 4
- 230000003647 oxidation Effects 0.000 title abstract description 3
- 238000007254 oxidation reaction Methods 0.000 title abstract description 3
- 239000007789 gas Substances 0.000 claims abstract description 49
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 239000010865 sewage Substances 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000001301 oxygen Substances 0.000 claims abstract description 13
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims abstract description 10
- 235000013619 trace mineral Nutrition 0.000 claims abstract description 5
- 239000011573 trace mineral Substances 0.000 claims abstract description 5
- 238000013022 venting Methods 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract 2
- 238000007599 discharging Methods 0.000 abstract 1
- 239000005416 organic matter Substances 0.000 abstract 1
- 239000010802 sludge Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 13
- 238000012545 processing Methods 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 8
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 7
- 241000894006 Bacteria Species 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 241000205011 Methanothrix Species 0.000 description 4
- 241000192023 Sarcina Species 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 241001453382 Nitrosomonadales Species 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000003851 biochemical process Effects 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229920002401 polyacrylamide Polymers 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical class [N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000035479 physiological effects, processes and functions Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000002352 surface water 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
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/22—O2
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/38—Gas flow rate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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)
Abstract
The invention discloses a device using AB-ASBR reactors to start anaerobic ammonia oxidation. The device comprises a sewage tank, a front-section reaction device and a rear-section reaction device. Each of the front-section reaction device and the rear-section reaction device comprises an ASBR reactor, a gas collecting device, a miniature vacuum pump, a time-control switch, a gas flowmeter, a pH measuring instrument, a dissolved oxygen measuring instrument and a temperature control device. The water outlet of the front-section ASBR reactor is connected with the water inlet of the rear-section ASBR reactor. The height ratio and diameter ratio of the front-section ASBR reactor to the rear-section ASBR reactor are 2-3. A gas outlet and a trace element adding port are formed in the top end of each of the front-section ASBR reactor and the rear-section ASBR reactor. A water inlet and a water outlet are respectively formed in the bottom side of each of the front-section ASBR reactor and the rear-section ASBR reactor. The bottom center of each of the front-section ASBR reactor and the rear-section ASBR reactor is provided with a gas circulation inlet and an aeration head, and the gas circulation inlet is arranged below the aeration head. An emptying valve and a mud discharging valve are further arranged at the bottom of each of the front-section ASBR reactor and the rear-section ASBR reactor. By the device, high-concentration organic matter can be degraded under an anaerobic condition while ammonia and nitrogen in sewage can be removed, sewage treatment efficiency is increased evidently, and treatment cost is lowered.
Description
Technical field
The present invention relates to a kind of device of AB-ASBR reactor start-up Anammox, belong to sewage sludge biologic treating technique field.
Background technology
China's ammonia nitrogen quantity discharged, far beyond the environmental capacity of receiving water body, becomes the primary index affecting surface water quality of water environment more than COD, and is listed in overall control index in " 12 " period.Ammonia nitrogen is cut down technique and is mainly divided into physico-chemical process and biochemical process two class.Physico-chemical process process cost of investment is high, and working cost is high, easily causes secondary pollution.Biochemical process processing cost is low, and secondary pollution is few, but treatment effect has to be hoisted.Traditional biological denitrification process generally can reach 70%-80% to ammonia nitrogen removal frank.Select suitable biochemical processing process, by regulate and control operation, ammonia nitrogen removal frank Be very effective can be made to improve, and reduce processing costs.
Domestic existing sewage biological treatment system carrys out supplementary carbon source demand often through adding outer carbon source, and this both added processing cost, exacerbated again CO in water factory
2discharge and a large amount of generations of excess sludge.Anammox treatment process, compared with traditional biological denitride technology, does not need additional organic carbon source; Do not need to add acid-base neutralisation reagent, avoid causing secondary pollution; Consume energy low; Sludge yield is few.According to domestic and international relevant report, the startup of Anammox reaction makes some progress, but the anaerobic ammonia oxidizing bacteria generation cycle is long, differs greatly start time for different reactor.The ASBR technique having realized Anammox reaction has following shortcoming: 1. flora advantage is unstable, and processing efficiency is not high.Intermittent fermentation is carried out in ASBR, along with initial matrix constantly shifts to intermediate product, in reactor, the composition of microorganism and dominant population also constantly substitute thereupon, and make the sarcina methanica in ASBR reactor and methanothrix sp all be difficult to stablize, respective biochemical advantage cannot give full play to.2. economic potential needs to be excavated further, and operation cost is higher.Be dominant bacteria mainly with methanothrix sp greatly due to the anaerobic grain sludge that formed in ASBR reactor, sacrifice the function that sarcina methanica matrix utilizes speed high, limit the raising of ASBR organic loading.For ensureing the normal operation of ASBR reactor, the normal measure adopting reduction design loading, to ensure that reactor easily keeps the balance between acid-producing bacteria and methanogen under relatively low load, because of the at utmost minimizing of the raising and initial cost which limit reactor volume load.
Summary of the invention
The object of this invention is to provide a kind of device of AB-ASBR reactor start-up Anammox, this device can realize the removal to ammonia nitrogen in waste water while high-enriched organics is removed, and improves sewage treating efficiency, reduces processing cost.
A device for AB-ASBR reactor start-up Anammox, comprising: sewage lagoon, leading portion reaction unit and back segment reaction unit;
Leading portion reaction unit comprises leading portion ASBR reactor, gas extractor, minipump, time switch, gas meter, pH determinator, dissolved oxygen meter and temperature control unit;
Back segment reaction unit comprises back segment ASBR reactor, gas extractor, minipump, time switch, gas meter, pH determinator, dissolved oxygen meter and temperature control unit;
Height and the diameter ratio of front and rear sections ASBR reactor are 2-3; Front and rear sections ASBR reactor top is equipped with venting port and trace element adds mouth, the bottom side of front and rear sections ASBR reactor is provided with water-in and water port respectively, the bottom centre of front and rear sections ASBR reactor is equipped with gas circulation entrance and aeration head, and gas circulation entrance is arranged on below aeration head; The bottom of front and rear sections ASBR reactor is equipped with exhaust-valve and mud valve; Venting port is connected with gas extractor by airway, gas extractor is connected with minipump inlet end by airway, minipump controls to open by time switch, the outlet side of minipump is connected with gas meter inlet end, and gas meter outlet side is connected with gas circulation entrance;
Sewage lagoon is connected with the water-in of leading portion ASBR reactor; The water port of leading portion ASBR reactor is connected with the water-in of back segment ASBR reactor;
Start front and rear sections ASBR reactor: with municipal sewage plant's returned sluge for seed sludge, inject front and rear sections ASBR reactor, its sludge concentration is 3000-4000mg/L, cultivate with original volume load 0.2gCOD/ (Ld) and add appropriate flocculation agent polyacrylamide, under medium temperature condition, cultivating anaerobic grain sludge; In sewage lagoon, wastewater influent injection leading portion ASBR reactor adsorbs, and after absorption terminates, sewage enters back segment ASBR reactor and degrades; After having intake, open minipump by time switch interval, gas in airbag is sucked air chamber by minipump, is delivered to reactor bottom and stirs, make waste water fully contact mixing with mud, carry out absorption degradation reaction after pressurization;
After step of reaction stirs for the last time, time controller power supply is closed automatically, and reactor enters precipitate phase; Mixed solution precipitates under quiescent conditions, carries out solid-liquid separation; Open effluent switch, under making the effect of the supernatant liquor after precipitation at gas storage pressure, discharge reactor;
Measure the pH value of sewage in front and rear sections ASBR reactor, dissolved oxygen and water temperature respectively by pH determinator, dissolved oxygen meter and temperature control unit, make its pH value maintain 6.8-7.2, dissolved oxygen close to 0, water temperature maintains 35 ± 2 DEG C; Run 2-3 cycle every day, leading portion ASBR reactor each cycle comprises into water-absorption-sedimentation-draining-regeneration, and back segment ASBR reactor each cycle comprises into water-degraded-sedimentation-draining-idle; Run front and rear sections ASBR reactor under these conditions, improve organic concentration gradually to more than 5000mg/L, and realize granular sludge;
Start Anammox reaction: after realizing granular sludge, in leading portion ASBR reactor, add NH
4 +-N and NO
2 --N, starting point concentration is respectively 50mg/L and 40mg/L, and progressively improves, and increases gradient and is respectively 50mg/L and 20mg/L, make NH
4 +-N, NO
2 --N concentration increases to 550mg/L and 320mg/L respectively, finally realizes Anammox.
Know-why of the present invention is as follows:
Before, optionally cultivate respectively in rear two reactor and develop respective dominant bacteria, before making, rear two reactor is respectively with the technique of the mode operation of Adsorption-Biodegradation, this technique is the physiology characteristic different with methanothrix sp according to sarcina methanica, front, optionally cultivate respectively in rear two reactor and develop respective dominant bacteria, the granule sludge that to cultivate with sarcina methanica and anaerobic ammonia oxidizing bacteria in leading portion ASBR reactor be dominant bacteria, the granule sludge that to cultivate with methanothrix sp and anaerobic ammonia oxidizing bacteria in back segment ASBR reactor be dominant bacteria, the water inlet of back segment is the water outlet of leading portion, before making, rear two reactor under the load differed greatly respectively with the mode operation of Adsorption-Biodegradation.
The operational mode of AB-ASBR technique leading portion is " water inlet-absorption-sedimentation-draining-regeneration "; The operational mode of back segment is " water inlet-degraded-sedimentation-draining-idle ".In two reactor, the optimization of methane flora is by the raising of the increase and effluent quality that are conducive to AB-ASBR technique influent load.
Compared with prior art, the present invention has the following advantages:
1. the mode connected by two-stage anaerobic sequencing batch reactor ASBR is disposed of sewage, and achieve sludge immobilization, Anammox, denitrogenation while high ammonia-nitrogen wastewater under high-enriched organics condition, solves carbon source and add problem, reduce processing cost.
2. the coexisting of methanogen floras and Anammox flora, achieves the removal to ammonia nitrogen in waste water while high-enriched organics is removed, greatly improves sewage treating efficiency, save processing cost and floor space.
3.AB-ASBR anaerobic ammonia oxidation reactor successfully can start and have good processing power to ammonia nitrogen class waste water, and experiment shows NH
4 +-N and NO
2 -the concentration for the treatment of of-N can reach 550mg/L and 320mg/L respectively, and clearance is respectively up to 92% and 95%.
4. the aspect ratio that reactor is suitable too increases the contact area of mud and liquid, for adsorption provides good environment, accelerates adsorption process; After absorption regeneration 6.5h, NH
4 +-N and NO
2 --N concentration is down to lower level, shows the renewable activity recovery of mud, can enter next cycle circulation.
Accompanying drawing explanation
Fig. 1 is the structural representation of the device of AB-ASBR reactor start-up Anammox of the present invention.
Embodiment
Below in conjunction with accompanying drawing, method of the present invention is described in detail.
As shown in Figure 1, the device of a kind of AB-ASBR reactor start-up Anammox of the present invention, comprising: sewage lagoon 1, leading portion reaction unit and back segment reaction unit;
A device for AB-ASBR reactor start-up Anammox, comprising: sewage lagoon 1, leading portion reaction unit and back segment reaction unit;
Leading portion reaction unit comprises leading portion ASBR reactor 2, gas extractor 42, minipump 52, time switch 62, gas meter 72, pH determinator 82, dissolved oxygen meter 92 and temperature control unit 102;
Back segment reaction unit comprises back segment ASBR reactor 3, gas extractor 43, minipump 53, time switch 63, gas meter 73, pH determinator 83, dissolved oxygen meter 93 and temperature control unit 103;
In leading portion reaction unit, the height of leading portion ASBR reactor 2 and diameter are than being 2-3; Leading portion ASBR reactor 2 top is provided with venting port 112, trace element adds mouth 122, the bottom side of leading portion ASBR reactor 2 is respectively equipped with water-in 132 and water port 142, the bottom centre of leading portion ASBR reactor 2 is provided with gas circulation entrance 152 and aeration head 162, and gas circulation entrance 152 is arranged on below aeration head 162; The bottom of leading portion ASBR reactor 2 is also provided with exhaust-valve 172 and mud valve 182; Venting port 112 is connected with gas extractor 42 by airway, gas extractor 42 is connected with minipump 52 inlet end by airway, minipump 52 controls to open by time switch 62, the outlet side of minipump 52 is connected with gas meter 72 inlet end, and gas meter 72 outlet side is connected with gas circulation entrance 152;
In back segment reaction unit, the height of back segment ASBR reactor 3 and diameter are than being 2-3; Back segment ASBR reactor 3 top is provided with venting port 113, trace element adds mouth 123, the bottom side of back segment ASBR reactor 3 is respectively equipped with water-in 133 and water port 143, the bottom centre of back segment ASBR reactor 3 is provided with gas circulation entrance 153 and aeration head 163, and gas circulation entrance 153 is arranged on below aeration head 163; The bottom of back segment ASBR reactor 3 is also provided with exhaust-valve 173 and mud valve 183; Venting port 113 is connected with gas extractor 43 by airway, gas extractor 43 is connected with minipump 53 inlet end by airway, minipump 53 controls to open by time switch 63, the outlet side of minipump 53 is connected with gas meter 73 inlet end, and gas meter 73 outlet side is connected with gas circulation entrance 153;
Sewage lagoon 1 is connected with the water-in 132 of leading portion ASBR reactor 2; The water port 142 of leading portion ASBR reactor 2 is connected with the water-in 133 of back segment ASBR reactor 3;
Start front and rear sections ASBR reactor: with municipal sewage plant's returned sluge for seed sludge, inject front and rear sections ASBR reactor, its sludge concentration is 3000-4000mg/L, cultivate with original volume load 0.2gCOD/ (Ld) and add appropriate flocculation agent polyacrylamide, under medium temperature condition, cultivating anaerobic grain sludge; In sewage lagoon 1, wastewater influent injection leading portion ASBR reactor 2 adsorbs, and after absorption terminates, sewage enters back segment ASBR reactor 3 and degrades; After having intake, open minipump 83 by time switch 43 interval, gas in airbag is sucked air chamber by minipump, is delivered to reactor bottom and stirs, make waste water fully contact mixing with mud, carry out absorption degradation reaction after pressurization;
After step of reaction stirs for the last time, time controller power supply is closed automatically, and reactor enters precipitate phase; Mixed solution precipitates under quiescent conditions, carries out solid-liquid separation;
Open effluent switch, under making the effect of the supernatant liquor after precipitation at gas storage pressure, discharge reactor.
For ensureing that reactor is in the environment of anaerobism, reactor own biological aerogenesis is utilized to carry out pneumatic agitation;
Measure the pH value of sewage in front and rear sections ASBR reactor, dissolved oxygen and water temperature respectively by pH determinator, dissolved oxygen meter and temperature control unit, make its pH value maintain 6.8-7.2, dissolved oxygen close to 0, water temperature maintains 35 ± 2 DEG C; Run 2-3 cycle every day, leading portion ASBR reactor 2 each cycle comprises into water-absorption-sedimentation-draining-regeneration, and back segment ASBR reactor 3 each cycle comprises into water-degraded-sedimentation-draining-idle; Run front and rear sections ASBR reactor under these conditions, improve organic concentration gradually to more than 5000mg/L, and realize granular sludge;
Start Anammox reaction: after realizing granular sludge, in leading portion ASBR reactor, add NH
4 +-N and NO
2 --N, starting point concentration is respectively 50mg/L and 40mg/L, and progressively improves, and increases gradient and is respectively 50mg/L and 20mg/L, make NH
4 +-N, NO
2 --N concentration increases to 550mg/L and 320mg/L respectively, finally realizes Anammox.
Claims (1)
1. a device for AB-ASBR reactor start-up Anammox, is characterized in that comprising sewage lagoon (1), leading portion reaction unit and back segment reaction unit;
Leading portion reaction unit comprises leading portion ASBR reactor (2), gas extractor (42), minipump (52), time switch (62), gas meter (72), pH determinator (82), dissolved oxygen meter (92) and temperature control unit (102);
Back segment reaction unit comprises back segment ASBR reactor (3), gas extractor (43), minipump (53), time switch (63), gas meter (73), pH determinator (83), dissolved oxygen meter (93) and temperature control unit (103);
The height of leading portion ASBR reactor (2) and back segment ASBR reactor (3) is 2-3 with diameter ratio; Leading portion ASBR reactor (2) and back segment ASBR reactor (3) top is equipped with venting port and trace element adds mouth, the bottom side of leading portion ASBR reactor (2) and back segment ASBR reactor (3) is provided with water-in and water port respectively, the bottom centre of leading portion ASBR reactor (2) and back segment ASBR reactor (3) is equipped with gas circulation entrance and aeration head, and gas circulation entrance is arranged on below aeration head; The bottom of leading portion ASBR reactor (2) and back segment ASBR reactor (3) is equipped with exhaust-valve and mud valve; Venting port is connected with gas extractor by airway, gas extractor is connected with minipump inlet end by airway, minipump controls to open by time switch, the outlet side of minipump is connected with gas meter inlet end, and gas meter outlet side is connected with gas circulation entrance;
Sewage lagoon (1) is connected with the water-in (132) of leading portion ASBR reactor (2); The water port (142) of leading portion ASBR reactor (2) is connected with the water-in (133) of back segment ASBR reactor (3).
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105906042A (en) * | 2016-06-09 | 2016-08-31 | 北京工业大学 | Strictly anaerobic reaction device applicable to anammox reaction and operation method |
| CN107381806A (en) * | 2017-09-07 | 2017-11-24 | 中南大学 | The water feed apparatus and method of a kind of anaerobic reactor |
| CN107771615A (en) * | 2017-11-24 | 2018-03-09 | 重庆蕊福农食用菌种植有限公司 | Multi-functional strain fermentation tank |
| CN110127841A (en) * | 2019-04-19 | 2019-08-16 | 湖北威尔达海绵城市建设有限公司 | A kind of integrated effluent disposal system |
| CN111908734A (en) * | 2020-08-28 | 2020-11-10 | 桂林理工大学 | AB process operation method based on anaerobic ammonia oxidation |
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