CN210340626U - Blue algae deep dehydration wastewater treatment system - Google Patents
Blue algae deep dehydration wastewater treatment system Download PDFInfo
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- CN210340626U CN210340626U CN201921051494.0U CN201921051494U CN210340626U CN 210340626 U CN210340626 U CN 210340626U CN 201921051494 U CN201921051494 U CN 201921051494U CN 210340626 U CN210340626 U CN 210340626U
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- 230000018044 dehydration Effects 0.000 title claims abstract description 28
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 28
- 241000195493 Cryptophyta Species 0.000 title claims description 32
- 238000004065 wastewater treatment Methods 0.000 title claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 97
- 239000010802 sludge Substances 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 239000012528 membrane Substances 0.000 claims abstract description 20
- 238000002156 mixing Methods 0.000 claims abstract description 20
- 238000004062 sedimentation Methods 0.000 claims abstract description 19
- 238000010992 reflux Methods 0.000 claims description 49
- 238000005345 coagulation Methods 0.000 claims description 20
- 230000015271 coagulation Effects 0.000 claims description 20
- 239000002351 wastewater Substances 0.000 claims description 15
- 230000001105 regulatory effect Effects 0.000 claims description 9
- 239000000701 coagulant Substances 0.000 claims description 7
- 239000008394 flocculating agent Substances 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 239000010865 sewage Substances 0.000 abstract description 10
- 238000000034 method Methods 0.000 abstract description 9
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- 229910052760 oxygen Inorganic materials 0.000 abstract description 4
- 239000001301 oxygen Substances 0.000 abstract description 4
- 206010021143 Hypoxia Diseases 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 230000008676 import Effects 0.000 abstract 3
- 208000005156 Dehydration Diseases 0.000 description 22
- 239000007788 liquid Substances 0.000 description 10
- 239000011575 calcium Substances 0.000 description 8
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 7
- 229910000019 calcium carbonate Inorganic materials 0.000 description 6
- 244000005700 microbiome Species 0.000 description 6
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- 229910001424 calcium ion Inorganic materials 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000012851 eutrophication Methods 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
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- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
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- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a blue alga degree of depth dehydration effluent disposal system, it includes the equalizing basin that meets through the pipeline order, mix the pond, coagulate the pond, the inclined plate sedimentation tank, the anaerobism intake chamber, upward flow formula anaerobism sludge impoundment, the oxygen deficiency pond, good oxygen pond and membrane biological reaction pond, the backward flow export in membrane biological reaction pond connects the backward flow import in good oxygen pond through the backflow pipeline, the backward flow export in good oxygen pond connects the backward flow import in oxygen deficiency pond through the backflow pipeline, the backward flow export in upward flow formula anaerobism sludge impoundment connects the backward flow import of mixing the pond through the backflow pipeline. The utility model solves the problems of low COD removal rate, Ca removal rate and the like in the prior art2+Get rid of the degree of difficulty big and the treatment depth is not enough, makes the process the utility model discloses a system and technology after handlingThe water meets the water quality standard of sewage discharged into urban sewers.
Description
Technical Field
The utility model relates to a blue alga degree of depth dehydration effluent disposal system, the utility model belongs to the technical field of sewage treatment system.
Background
In 2017, in 5-6 months, severe blue-green algae pollution is caused by outbreak of Taihu lake of Jiangsu in China, so that the tap water pollution of the whole city without tin is caused. In recent years, due to rapid development of industry, over 66% of lakes and reservoirs in China are in eutrophication level, wherein the eutrophication and the over-eutrophication account for 22%. The direct consequence of lake eutrophication is that blue algae is propagated in large quantity, the water quality is deteriorated due to the blue algae outbreak, the lake water source can not be used, and the water use crisis is easily caused if no emergency water source exists locally.
At present, the blue algae is mainly treated by adopting a salvaging mode in China and then further treated. The water content of the salvaged blue algae is about 99.4 percent, the water content of the blue algae after being treated in the algae-water separation station is about 85 to 90 percent, the transportation cost is high, and the subsequent treatment and disposal difficulty is high. In recent years, the blue algae mud deep dehydration technology is continuously developed, the volume and weight of the blue algae mud after deep dehydration are about 50-60%, the transportation cost is reduced, and the subsequent treatment difficulty is reduced.
Through search, Chinese invention patents with patent number ZL201811322717.2 and grant publication number CN109336360A disclose a blue algae deep dehydration method and a power generation energy method thereof. The blue algae deep dehydration method comprises modification treatment and dehydration treatment, wherein the modification treatment is to add a modification treatment agent into blue algae and algae slurry, and the modification treatment agent is one or more of calcium oxide, calcium hydroxide, ferric trichloride and polyaluminium chloride. The water content of the blue algae can be reduced to below 60 percent, the method is simple and can realize deep dehydration of the blue algae, and the blue algae cake obtained after dehydration can be incinerated to generate power after being added into an incinerated substance, thereby realizing the energy regeneration of the blue algae. But the wastewater generated by the dehydration treatment of the technology adopts the addition of catalysts such as ozone, ferric oxide and the like to remove part of COD (namely chemical oxygen demand) in the wastewaterThe removal efficiency of COD is limited, and a medicament needs to be added; if the dehydration modifying agent is calcium oxide or calcium hydroxide, Ca in the dehydration waste liquid2+Scaling and other adverse effects are easy to generate in the subsequent biochemical treatment, and the subsequent biochemical treatment is not facilitated; the wastewater treatment depth is not enough, and a denitrification unit is not provided, so that the water quality standard of sewage discharged into urban sewers can not be met.
Disclosure of Invention
The utility model aims to overcome the defects in the prior art and provide a method which can improve the removal rate of COD and reduce Ca2+Difficulty of removal and increase of Ca2+A blue algae deep dehydration wastewater treatment system for deep treatment.
According to the technical scheme provided by the utility model, the blue algae deep dehydration wastewater treatment system comprises a regulating tank, a mixing tank, a coagulation tank, an inclined plate sedimentation tank, an anaerobic water inlet tank, an upflow anaerobic sludge tank, an anoxic tank, an aerobic tank and a membrane biological reaction tank;
a flocculating agent adding pipe and a coagulating agent adding pipe are arranged on the coagulation tank, and a high-temperature steam access pipe and an acid access pipe are arranged on the anaerobic water inlet tank;
the blue algae dewatering waste water pipe is connected with the water inlet of the regulating tank, the water outlet of the regulating tank is connected with the water inlet of the mixing tank through a pipeline, the water outlet of the mixing tank is connected with the water inlet of the coagulation tank through a pipeline, the water outlet of the coagulation tank is connected with the water inlet of the inclined plate sedimentation tank through a pipeline, the water outlet of the inclined plate sedimentation tank is connected with the water inlet of the anaerobic water inlet tank through a pipeline, the water outlet of the anaerobic water inlet tank is divided into two pipelines, one pipeline is connected with the first water inlet of the upflow anaerobic sludge tank, the other pipeline exceeds the second water inlet of the anoxic tank, the first water outlet of the upflow anaerobic sludge tank is connected with the first water inlet of the anoxic tank through a pipeline, the water outlet of the anoxic tank is connected with the water inlet of the aerobic tank through a pipeline, the water outlet of the aerobic tank is connected with the water inlet of the membrane biological, the reflux outlet of the aerobic tank is connected with the reflux inlet of the anoxic tank through a reflux pipeline, and the reflux outlet of the upflow anaerobic sludge tank is connected with the reflux inlet of the mixing tank through a reflux pipeline.
The reflux ratio of a reflux outlet of the upflow anaerobic sludge tank is 80-100%.
The reflux ratio of the reflux outlet of the aerobic tank is 200-300%.
The reflux ratio of the reflux outlet of the membrane biological reaction tank is 300-400%.
The utility model solves the problems of low COD removal rate, Ca removal rate and the like in the prior art2+The difficulty of removal is big and the treatment depth is not enough, so that the water treated by the system and the process of the utility model meets the water quality standard of sewage discharge into urban sewers.
Drawings
Fig. 1 is a schematic diagram of the system of the present invention.
Detailed Description
The present invention will be further described with reference to the following specific embodiments.
In the present invention, PAC is an english abbreviation of polyaluminium chloride. PAM is an english abbreviation for polyacrylamide.
The utility model discloses a blue algae deep dehydration wastewater treatment system, which comprises an adjusting tank 1, a mixing tank 2, a coagulation tank 3, an inclined plate sedimentation tank 4, an anaerobic water inlet tank 5, an upflow anaerobic sludge tank 6, an anoxic tank 7, an aerobic tank 8 and a membrane biological reaction tank 9;
a flocculating agent adding pipe 31 and a coagulating agent adding pipe 32 are arranged on the coagulation tank 3, and a high-temperature steam access pipe 51 and an acid access pipe 52 are arranged on the anaerobic water inlet tank 5;
the blue algae dewatering waste water pipe is connected with the water inlet of the adjusting tank 1, the water outlet of the adjusting tank 1 is connected with the water inlet of the mixing tank 2 through a pipeline, the water outlet of the mixing tank 2 is connected with the water inlet of the coagulation tank 3 through a pipeline, the water outlet of the coagulation tank 3 is connected with the water inlet of the inclined plate sedimentation tank 4 through a pipeline, the water outlet of the inclined plate sedimentation tank 4 is connected with the water inlet of the anaerobic water inlet tank 5 through a pipeline, the water outlet of the anaerobic water inlet tank 5 is divided into two pipelines, one pipeline is connected with the first water inlet of the upflow anaerobic sludge tank 6, the other pipeline is connected with the second water inlet of the anoxic tank 7 in a surpassing mode, the first water outlet of the upflow anaerobic sludge tank 6 is connected with the first water inlet of the anoxic tank 7 through a pipeline, the water outlet of the anoxic tank 7 is connected with the water inlet of the aerobic tank 8 through, the reflux outlet of the membrane biological reaction tank 9 is connected with the reflux inlet of the aerobic tank 8 through a reflux pipeline, the reflux outlet of the aerobic tank 8 is connected with the reflux inlet of the anoxic tank 7 through a reflux pipeline, and the reflux outlet of the upflow anaerobic sludge tank 6 is connected with the reflux inlet of the mixing tank 2 through a reflux pipeline.
The utility model discloses well equalizing basin 1's design parameter:
designing scale: 3600m3/d；
Size: 37.8 × 38.0 × 5.5 m;
residence time: 48 h;
reaction form: blue algae press filtrate
The main equipment is as follows: mechanical stirrer, submersible sewage pump.
The utility model discloses well design parameter who mixes pond 2:
design Scale 3600m3/d；
Size: 16.3X 7.9X 5.5 m;
residence time: 4.3 h;
reaction form: UASB reflux liquid
The main equipment is as follows: a mechanical stirrer.
The utility model discloses well coagulation tank 3's design parameter:
designing scale: 3600m3/d；
Size: 13.4X 6.8X 5.5 m;
residence time: 3 h;
reaction type: adding PAC and PAM.
The utility model discloses well swash plate sedimentation tank 4's design parameter:
designing scale: 3600m3/d；
Size: 4.2X 8.8X 5.5 m;
the number of groups: group 3
Residence time: 3.7 h;
the main equipment is as follows: a sloping plate sedimentation tank and a sludge discharge pump.
The utility model discloses well anaerobism intake pool 5's design parameter:
designing scale: 3600m3/d；
Size: 16.0 × 7.6 × 5.5 m;
the number of groups: 2 groups of
Residence time: 8.1 h;
reaction form: steam heating and pH adjustment;
the main equipment is as follows: mechanical stirrer, anaerobic feeding pump and overtaking pump.
The utility model discloses well UASB reactor
The UASB reactor system is mainly used for removing a large amount of organic matters in the wastewater and greatly reducing the load of a subsequent biological treatment unit. 100 percent of effluent of the anaerobic reactor flows back to the pretreatment tank, and 100 percent of effluent enters a subsequent AO-MBR tank for denitrification reaction.
Designing parameters:
designing scale: 3600m3/d；
Size: phi 10X 19 m;
quantity: 2, the number of the cells is 2;
residence time: 18.9 h;
volume load: 4.59kgCODcr/(m3·d)；
The reactor temperature: 30-35 ℃;
the main equipment is as follows: a feeding pump, a circulating pump and an anaerobic sludge pump.
The utility model discloses well oxygen deficiency pond 7's design parameter:
designing scale: 3600m3/d，
Single group size: 15.0 × 10.0 × 5.5 m;
quantity: 4 groups;
residence time: 20 h;
the main equipment is as follows: a mechanical stirrer;
the design parameters of the middle aerobic tank 8 of the utility model are as follows:
designing scale: 3600m3/d；
Single group size: 16.5 × 10.0 × 5.5 m;
quantity: 4 groups;
residence time: 22 h;
the main equipment is as follows: jet aerator, jet circulating pump, nitrifying liquid reflux pump and blower.
The utility model discloses well membrane biological reaction tank 9's design parameter:
designing scale: 3600m3/d；
Single group size: 18.0X 3.0X 4.5 m;
quantity: 2, group (b);
residence time: 2.5 h;
the main equipment is as follows: membrane module, product water pump, backwash pump, sludge reflux pump, air-blower, medicine system.
The utility model discloses well clean water basin design parameter:
designing scale: 3600m3/d，
Single group size: 4.0 × 3.0 × 5.5 m;
quantity: 1 group;
residence time: 0.4 h.
The reflux ratio of the membrane biological reaction tank 9 to the aerobic tank 8 is 300 percent, the reflux ratio of the nitrifying liquid in the aerobic tank 8 to the anoxic tank 7 is 400 percent, and simultaneously, the concentration of nitrate and sludge is supplemented.
A wastewater treatment method for deep dehydration of blue algae comprises the following steps:
a. blue algae deep dehydration wastewater is conveyed into the regulating reservoir 1 through a submersible sewage pump and a pipeline;
b. wastewater discharged from a water outlet of the adjusting tank 1 is lifted into the mixing tank 2 through a submersible sewage pump and a pipeline, reflux liquid conveyed from a reflux outlet of the upflow anaerobic sludge tank 6 to a reflux inlet of the mixing tank 2 through a pipeline is mixed with the wastewater in the mixing tank 2, and CO in the reflux liquid3 2-With Ca in blue algae deep dehydration wastewater2+Formation of CaCO3Floc particles;
c. adding flocculant PAM into coagulation tank 3 from flocculant adding pipe 31, adding coagulant PAC containing CaCO into coagulation tank 3 from coagulant adding pipe 323The wastewater of the floc particles is conveyed from the mixing tank 2 to the coagulation tank 3, and is coagulated in the flocculant PAMBy action of agents PAC, CaCO3The floc particles become more compact and have larger particle size;
d. containing CaCO3Conveying the flocculated wastewater from the coagulation tank 3 to an inclined plate sedimentation tank 4 for sedimentation, discharging the calcium-containing sludge after sedimentation, conveying the calcium-containing sludge to a deep dehydration system for dehydration, and then treating the calcium-containing sludge;
e. conveying the supernatant subjected to precipitation to an anaerobic water inlet tank 5, introducing high-temperature steam into the anaerobic water inlet tank 5 through a high-temperature steam access pipe 51 to raise the temperature of the supernatant to 30-35 ℃, introducing hydrochloric acid into the anaerobic water inlet tank 5 through an acid access pipe 52, and controlling the pH value of the supernatant to 6.5-7.5;
clear liquid in the anaerobic water inlet tank 5 enters an up-flow anaerobic sludge tank 6, and anaerobic fermentation is carried out in the up-flow anaerobic sludge tank 6;
the sewage after anaerobic fermentation enters an anoxic tank 7, NO in the sewage which flows back to the anoxic tank 7 from an aerobic tank 8 is subjected to denitrification of microorganisms in the anoxic tank 73Reduction of-N to N2Completing the removal of nitrogen; if the carbon source contained in the anoxic tank 7 is insufficient, the effluent of the anaerobic water inlet tank 5 is transcend to the anoxic tank 7;
the effluent of the anoxic tank 7 enters an aerobic tank 8, sludge containing microorganisms in a membrane biological reaction tank 9 flows back to the aerobic tank 8, and NH in the sewage is subjected to nitrification of the microorganisms3Oxidation of-N to NO3-N；
The effluent of the aerobic tank 8 enters a membrane biological reaction tank 9 to complete the separation of water and sludge containing microorganisms, the separated water is discharged, and the sludge containing the microorganisms flows back to the aerobic tank 8.
The coagulant is polyaluminium chloride PAC, and the adding amount of the coagulant is 20-40 mg/L.
The flocculating agents are respectively polyacrylamide PAM, and the adding amount of the flocculating agents is 1-3 mg/L.
The reflux ratio of the reflux outlet of the upflow anaerobic sludge tank 6 is 80-100%.
The reflux ratio of the reflux outlet of the aerobic tank 8 is 200-300%.
The reflux ratio of the reflux outlet of the membrane biological reaction tank 9 is 300-400%.
The mixing tank 2 is arranged behind the regulating tank 1 and aims to uniformly mix the reflux of the upflow anaerobic reactor (6) with the inlet water of the regulating tank to generate CaCO3(ii) a The inclined plate sedimentation tank 4 is arranged behind the coagulation tank 3 for accelerating CaCO3Precipitating to complete sludge-water separation; an anaerobic water inlet tank 5 is arranged behind the inclined plate sedimentation tank 4 for adjusting the temperature and the pH value; an upflow anaerobic reactor 6 is arranged behind the anaerobic water inlet tank 5, aiming at removing pollutants such as COD and the like in the inlet water; an anoxic tank 7 is arranged behind the upflow anaerobic reactor 6 to utilize the microbial action to remove NO in the reflux liquid of the aerobic tank 83Reduction of-N to N2Removing N-type pollutants; the aerobic tank 8 is arranged behind the anoxic tank 7 for removing NH in the inlet water3Oxidation of-N to NO3N, refluxing to the anoxic tank 7 to remove the N pollutants; the membrane biological reaction tank 9 is arranged behind the aerobic tank 8 for separating mud (microorganism) from clean water.
The purpose of the reflux of the upflow anaerobic sludge tank 6 to the mixing tank 2 is to ensure that CO in the reflux liquid3 2-With Ca in blue algae deep dehydration wastewater2+Formation of CaCO3The floccule particles pass through a coagulation tank 3 and an inclined plate sedimentation tank 4 to discharge mud, and the Ca in the wastewater is completed2+Removing; the purpose of the reflux of the aerobic tank 8 to the anoxic tank 7 is to lead NO in the water in the aerobic tank3-N reflux of NO to anoxic tank 7 by microbial action3Reduction of-N to N2Completing the removal of N-type pollutants; the purpose of the backflow from the membrane biological reaction tank 9 to the aerobic tank 8 is to supplement the sludge concentration in the aerobic tank; the purpose that the outlet of the anaerobic water inlet tank 5 exceeds the inlet of the anoxic tank 7 is to supplement microorganisms in the anoxic tank 7 by using nutrient substances in the inlet water and help to finish NO3Reduction of-N to N2And finishing the removal of the N-type pollutants.
To sum up, the utility model discloses pretreatment systems utilizes UASB reactor's backward flow liquid to get rid of the calcium ion in the waste water, avoids the influence of calcium ion to low reaches biochemical treatment. Meanwhile, a UASB reactor is used for removing a large amount of organic matters in the wastewater, so that the energy consumption is saved, and the biological treatment load of a subsequent AO-MBR tank is greatly reduced; the utility model discloses a waste water treatment process flow is complete, area is less, waste water treatment is effectual, resource recovery rate is high.
The treatment effect of the blue algae deep dehydration wastewater treatment process of the utility model is shown in the following table 1.
TABLE 1
In table 1, the pretreatment tank includes an adjusting tank 1, a mixing tank 2, a coagulation reaction tank 3, an inclined plate sedimentation tank 4, and an anaerobic water inlet tank 5.
The AO-MBR system comprises an aerobic tank 7, an anoxic tank 8 and a membrane biological reaction tank 9.
The above description is only an example of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the claims of the present invention.
Claims (4)
1. The utility model provides a blue alga degree of depth dehydration effluent disposal system which characterized by: comprises a regulating tank (1), a mixing tank (2), a coagulation tank (3), an inclined plate sedimentation tank (4), an anaerobic water inlet tank (5), an up-flow anaerobic sludge tank (6), an anoxic tank (7), an aerobic tank (8) and a membrane biological reaction tank (9);
a flocculating agent adding pipe (31) and a coagulating agent adding pipe (32) are arranged on the coagulation tank (3), and a high-temperature steam access pipe (51) and an acid access pipe (52) are arranged on the anaerobic water inlet tank (5);
the blue algae dewatering wastewater pipe is connected with the water inlet of the regulating tank (1), the water outlet of the regulating tank (1) is connected with the water inlet of the mixing tank (2) through a pipeline, the water outlet of the mixing tank (2) is connected with the water inlet of the coagulation tank (3) through a pipeline, the water outlet of the coagulation tank (3) is connected with the water inlet of the inclined plate sedimentation tank (4) through a pipeline, the water outlet of the inclined plate sedimentation tank (4) is connected with the water inlet of the anaerobic water inlet tank (5) through a pipeline, the water outlet of the anaerobic water inlet tank (5) is divided into two pipelines, one pipeline is connected with the first water inlet of the upflow anaerobic sludge tank (6), the other pipeline is connected with the second water inlet of the anoxic tank (7) in an overrunning manner, the first water outlet of the upflow anaerobic sludge tank (6) is connected with the first water inlet of the anoxic tank (7) through a pipeline, the water outlet of the anoxic tank (7) is connected with the water inlet of the aerobic tank (, the water outlet of the membrane biological reaction tank (9) is connected with a discharge pipe, the backflow outlet of the membrane biological reaction tank (9) is connected with the backflow inlet of the aerobic tank (8) through a backflow pipeline, the backflow outlet of the aerobic tank (8) is connected with the backflow inlet of the anoxic tank (7) through a backflow pipeline, and the backflow outlet of the upflow anaerobic sludge tank (6) is connected with the backflow inlet of the mixing tank (2) through a backflow pipeline.
2. The blue algae deep dehydration wastewater treatment system according to claim 1, characterized in that: the reflux ratio of the reflux outlet of the upflow anaerobic sludge tank (6) is 80-100%.
3. The blue algae deep dehydration wastewater treatment system according to claim 1, characterized in that: the reflux ratio of the reflux outlet of the aerobic tank (8) is 300-400%.
4. The blue algae deep dehydration wastewater treatment system according to claim 1, characterized in that: the reflux ratio of the reflux outlet of the membrane biological reaction tank (9) is 200-300%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110183066A (en) * | 2019-07-05 | 2019-08-30 | 无锡市政设计研究院有限公司 | Cyanobacteria deep dehydration waste water treatment system and technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110183066A (en) * | 2019-07-05 | 2019-08-30 | 无锡市政设计研究院有限公司 | Cyanobacteria deep dehydration waste water treatment system and technique |
| CN110183066B (en) * | 2019-07-05 | 2023-07-07 | 华昕设计集团有限公司 | Blue algae deep dehydration wastewater treatment system and process |
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