CN210635853U - Water body algal bloom treatment system - Google Patents
Water body algal bloom treatment system Download PDFInfo
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- CN210635853U CN210635853U CN201921508912.4U CN201921508912U CN210635853U CN 210635853 U CN210635853 U CN 210635853U CN 201921508912 U CN201921508912 U CN 201921508912U CN 210635853 U CN210635853 U CN 210635853U
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Abstract
The utility model provides a water algal bloom treatment system, system include oxidation condensation reaction tank, compound heterogeneous separator, denitrification reactor, broken wall reaction tank, ceramic membrane reactor, sludge thickening tank, pressure filter, and the delivery port of ceramic membrane reactor, sludge thickening tank's delivery port and the delivery port of pressure filter are connected with denitrification reactor respectively. The utility model realizes the unification of algae cell removal and long-term control of algal bloom, makes full use of the carbon source in the algae cells to carry out heterotrophic denitrification, avoids additional carbon source, and has higher efficiency compared with autotrophic denitrification; the method can be used as an on-site off-line treatment method, is easy to realize equipment, and can be designed in a buried manner; good treatment effect, small sludge output and low operation cost.
Description
Technical Field
The utility model belongs to the technical field of the water environment is administered, concretely relates to water algal bloom administers system.
Background
Many cities in China have water bodies such as landscape rivers, lakes and the like, and become important foundations of hydrophilic landscape, hydrophilic culture and livable cities. For a long time, because of source control and sewage interception, endogenous treatment, and lagged construction of basic facilities such as sponge cities, a plurality of urban water bodies show eutrophication characteristics, and large-area algal blooms appear in summer and autumn. The treatment of polluted rivers and lakes has important significance for guaranteeing the ecological health of water and maintaining the ecological diversity of water. Particularly, for polluted urban water, firstly, algae removal needs to be enhanced to quickly improve the sensory effect of the water, and in addition, pollutants such as nitrate, nitrogen, total nitrogen and the like need to be effectively removed, so that the method has important significance for continuously improving the water quality and realizing the recovery of the water function.
Autotrophic or heterotrophic denitrification is an important means for removing nitrate and total nitrogen. Autotrophic denitrification utilizes sulfur, hydrogen and the like as electron donors, has the advantages of no need of additional carbon sources and has the disadvantages of long generation time, long retention time and low treatment efficiency of microorganisms. The heterotrophic denitrifying bacteria have greatly improved treatment capacity compared with autotrophic bacteria, and have the defects of complex operation management due to the need of adding additional carbon sources such as acetic acid, ethanol, methanol and the like. Algae cells need to be removed in the process of treating the algae bloom water body, and the algae cells contain organic matters which can be possibly used as a carbon source of added heterotrophic bacteria if the organic matters can be fully utilized. However, it is necessary to perform systematic evaluation and scientific design to improve the microbial availability of carbon sources in algal cells and to effectively avoid total nitrogen release in the algal cells during the utilization of carbon sources.
The utility model provides a to above-mentioned problem, provide an alga in the time of "algal bloom" takes place for eutrophic urban water and strengthened getting rid of and nitrate, nitrogen, total nitrogen get rid of control method, realize that the algae cell gets rid of fast, quality of water improves and eutrophication risk control.
SUMMERY OF THE UTILITY MODEL
The utility model provides a to above-mentioned problem, provide a system that can effectively get rid of algal bloom and nitrate, nitrogen, total nitrogen.
In order to solve the technical problem, the utility model adopts the following technical scheme:
the water body algal bloom treatment system comprises an oxidation coagulation reaction tank, a composite multiphase separator communicated with a water outlet of the oxidation coagulation reaction tank, a denitrification reactor communicated with a water outlet of the composite multiphase separator, a wall breaking reaction tank communicated with a sludge discharge port of the composite multiphase separator, a ceramic membrane reactor communicated with an outlet of the wall breaking reaction tank, a sludge concentration tank communicated with a concentrated water outlet of the ceramic membrane reactor, and a filter press communicated with a sludge discharge port of the sludge concentration tank, wherein the water outlet of the ceramic membrane reactor, the water outlet of the sludge concentration tank and the water outlet of the filter press are respectively connected with the denitrification reactor.
Preferably, the water body algal bloom treatment system further comprises a first reagent adding system communicated with the oxidation coagulation reaction tank, a second reagent adding system communicated with a pipeline connecting the oxidation coagulation reaction tank and the composite multiphase separator, a third reagent adding system communicated with a pipeline connecting the composite multiphase separator and the wall breaking reaction tank, and a fourth reagent adding system communicated with a pipeline connecting the ceramic membrane reactor and the sludge concentration tank.
Further preferably, the first reagent dosing system comprises a plurality of storage tanks for storing different reagents, the second reagent dosing system comprises a plurality of storage tanks for storing different flocculants, the third reagent dosing system comprises one or more storage tanks for storing an oxidant, and the fourth reagent dosing system comprises a plurality of storage tanks for storing different flocculants.
Further preferably, a mixer is arranged on a pipeline connecting the oxidation coagulation reaction tank and the composite multiphase separator, and the mixer is positioned at the downstream of the connection position of the second medicament adding system and the pipeline.
Preferably, the composite multiphase separator comprises a barrel, a cyclone arranged at the lower part of the barrel, a flow baffle arranged in the barrel and positioned above the cyclone, a sludge concentration component arranged between the barrel and the cyclone, a plurality of inclined plates arranged in the barrel and positioned above the flow baffle, and a filler area arranged in the barrel and positioned above the inclined plates, wherein a water inlet of the composite multiphase separator is formed in the side part of the cyclone, a water outlet of the composite multiphase separator is formed in the top of the barrel, and a sludge discharge port is formed in the bottom of the cyclone and the barrel.
The composite multiphase separator realizes the function of cyclone centrifugation through a cyclone; the functions of destabilization, flocculation, sludge sedimentation, concentration, compression and the like of particles are completed through a sludge concentration part, a flow baffle plate and an inclined plate; the reactor can have the function of adsorbing and removing heavy metals and the like through the filler in the filler area, wherein the filler is one or more of hydroxyl iron oxide, activated alumina, zeolite, manganese oxide, iron-manganese composite oxide and ion exchange resin; the particle size range of the filler is 1-2 mm.
Wherein, the sludge concentration part comprises a stirrer, and the sludge is concentrated and compressed by a gravity concentration method through slow stirring of the stirrer.
Specifically, the inclined plates are arranged in parallel, and the extending direction of the inclined plates is intersected with the axial direction of the cylinder.
Preferably, the wall-breaking reaction tank comprises an ultraviolet region, an ultraviolet-ultrasonic synergistic region and an ultrasonic region which are sequentially arranged from an inlet to an outlet, and the volume ratio of the ultraviolet region to the ultraviolet-ultrasonic synergistic region to the ultrasonic region is 10-25: 2-5: 1.
Further preferably, ultraviolet lamps are arranged in the ultraviolet region and the ultraviolet-ultrasonic synergetic region, the length direction of lamp tubes of the ultraviolet lamps is perpendicular to the water flow direction, the distance between every two adjacent ultraviolet lamps is 2-10 cm, and the ultraviolet dose is 40-80 mJ/cm2。
Further preferably, the ultraviolet-ultrasonic cooperation area and the lower part of the ultrasonic area are provided with ultrasonic generators, the direction of ultrasonic waves emitted by the ultrasonic generators is perpendicular to the direction of water flow, and the dosage of the ultrasonic waves is 50-100 mJ/cm2。
Preferably, the ceramic membrane adopted by the ceramic membrane reactor is a microfiltration membrane with the membrane aperture of 0.05-0.45 microns or an ultrafiltration membrane with the retention capacity of 50-300 Kda.
Preferably, the filter press is a belt filter press or a plate and frame filter press; the denitrification reactor is an upflow anaerobic sludge blanket, an internal circulation anaerobic reactor, an anaerobic folded plate reactor or an anaerobic filtration blanket reactor.
The utility model discloses a method for water body algal bloom governing system administers water body algal bloom, including the following step:
(1) introducing the sewage to be treated into an oxidation coagulation reaction tank, and oxidizing and coagulating the sewage to be treated to remove algae by adding a medicament;
(2) adding a flocculating agent into the sewage treated in the step (1), introducing into a composite multiphase separator for solid-liquid separation, and introducing the effluent of the composite multiphase separator into a denitrification reactor;
(3) adding an oxidant into the algae-containing sludge discharged muddy water discharged from the composite multiphase separator, and introducing the mixture into a wall-breaking reaction tank for oxidation wall breaking;
(4) introducing the sludge water treated by the wall-breaking reaction tank into a ceramic membrane reactor for separation, and introducing the effluent of the ceramic membrane reactor into the denitrification reactor;
(5) adding a flocculating agent into the concentrated water of the ceramic membrane reactor, introducing the concentrated water into a sludge concentration tank for concentration, and introducing the clear liquid of the sludge concentration tank into the denitrification reactor;
(6) and the concentrated sludge of the sludge concentration tank is introduced into a filter press for filter pressing, and the pressure filtrate of the filter press is introduced into the denitrification reactor.
Preferably, the reagents adopted in the step (1) are a pre-oxidant, a ferrous salt aqueous solution and a ferric salt aqueous solution which are sequentially added, the adding time interval of the pre-oxidant and the ferrous salt aqueous solution is controlled to be 2-20 min, the adding time interval of the ferrous salt aqueous solution and the ferric salt aqueous solution is controlled to be 0-5 min, the ferric salt aqueous solution is added and then reacts for 10-20 min, and the mixture is discharged out of the oxidation coagulation reaction tank, wherein the pre-oxidant is one or more of potassium permanganate, sodium hypochlorite, ozone and calcium dioxide; the dosage of the pre-oxidant is the pre-oxidant and algaeThe ratio of the cells is 0.5-5 × 103mg preoxidant: 0.1 to 5X 109Individual algal cells; the ferrous salt is ferrous sulfate and/or ferrous chloride; the dosage of the ferrous salt is that the ratio of the ferrous salt to the algal cells is 2-20 mg: 0.1 to 5X 109Individual algal cells; the ferric salt is one or a mixture of more than one of ferric sulfate, ferric chloride, polyferric chloride and polyferric sulfate; the mole ratio of the ferric salt to the ferrous salt is 0: 1-1: 1.
preferably, the flocculating agents added in the step (2) and the step (5) are polyaluminium chloride and polyacrylamide, the dosage of the polyaluminium chloride is 20-27 mg/L, and the dosage of the polyacrylamide is 0.5-1 mg/L; and controlling the retention time of the mixture of the flocculating agent and the sewage in the composite multiphase separator to be 35-40 min.
Preferably, the oxidant added in step (3) is one or more of oxygen, chlorine dioxide, hydrogen peroxide and ozone mixed solution; the dosage of the oxidant is 100-250 mg/g algae cell dry solid, or 5-15g/g total nitrogen.
Preferably, the retention time of the water to be treated in the sludge concentration tank is controlled to be 30-60 min, and the retention time of the water to be treated in the denitrification reactor is controlled to be 2-6 h.
The technical principle of the utility model lies in: firstly, the method of the utility model ZL 201210158949.5 is used for moderate oxidation-synergistic coagulation strengthening algae removal. Specifically, a pre-oxidizing agent which has certain capacities of inactivating and inhibiting the activities of algae cells and is weak in oxidizing and breaking the cell walls of the algae is used for pre-oxidizing treatment, such as potassium permanganate, and the pre-oxidizing agent does not significantly cause the release of substances in algae cells; in addition, In situ formation of In situ MnO by potassium permanganate reduction reaction2Can be deposited on the surface of algae cells and improve the sedimentation performance of the algae cells. The subsequent addition of ferrous salt water solution and ferric salt water solution reduces the excessive pre-oxidant to stop pre-oxidation to control the continuous release of organic matter in algae cell and generate new ferriteFerric iron and ferric salt as coagulant to produce coagulation, ferric salt capable of neutralizing algae cell surface potential directly and In situ produced In situ by ferric salt hydrolysis reaction3Can also deposit on the surface of the algae cells to improve the surface potential and the sedimentation performance.
And then, performing solid-liquid separation by using a composite multiphase separator, feeding the obtained algae-containing sludge into a wall-breaking reaction tank, and feeding the treated water into a denitrification reactor.
Carrying out oxidation wall breaking on the algae-containing sludge in a wall breaking reaction tank under the action of ultrasonic, ultraviolet and synergetic advanced oxidation, so that algae extracellular organic substances EOM and extracellular polymeric substances EPS fall off, and intracellular organic substances IOM are released into water; solid-liquid separation is carried out by adopting an immersed ceramic membrane reactor, wherein concentrated solution of the ceramic membrane reactor mainly comprises solid remains of algae cells and inorganic particles in raw water, and safe landfill disposal is carried out after concentration and filter pressing. The effluent of the ceramic membrane reactor, the effluent of the sludge concentration tank and the effluent of the filter press are supplemented into the denitrification reactor, so that the carbon source in the algae cells can be fully utilized for heterotrophic denitrification, the additional carbon source is avoided, and the efficiency is higher compared with the autotrophic denitrification.
Due to the implementation of the above technical scheme, compared with the prior art, the utility model have the following advantage:
1. the unification of algae cell removal and long-term control of algal bloom is realized;
2. the carbon source in the algae cells is fully utilized for heterotrophic denitrification, the additional carbon source is avoided, and the efficiency is higher compared with that of autotrophic denitrification;
3. as an on-site off-line treatment method, the method is easy to realize equipment and can be designed in a buried manner;
4. good treatment effect, small sludge output and low operation cost.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment;
FIG. 2 is a schematic diagram of the structure of the composite multiphase separator;
FIG. 3 is a side view of a wall broken reactor;
wherein, 1, oxidizing and condensing reaction tank; 2. a composite multiphase separator; 3. a denitrification reactor; 4. a wall breaking reaction tank; 5. a ceramic membrane reactor; 6. a sludge concentration tank; 7. a filter press; 8. a first agent dosing system; 9. a second agent dosing system; 10. a third agent dosing system; 11. a fourth agent dosing system; 12. a storage tank; 13. a mixer; 21. a barrel; 22. a swirler; 23. a flow baffle plate; 24. a sludge concentration section; 25. a sloping plate; 26. a filler zone; 41. an ultraviolet region; 42. an ultraviolet-ultrasonic synergistic region; 43. an ultrasonic zone; 44. an ultraviolet lamp; 45. an ultrasonic generator.
Detailed Description
The following examples are intended to illustrate several embodiments of the present invention, but do not limit the invention to these embodiments. It will be recognized by those skilled in the art that the present invention encompasses all alternatives, modifications, and equivalents as may be included within the scope of the claims.
The structures and the like which are not described in detail in the present invention are conventional technical means in the field.
The structure of the water body algal bloom treatment system of the embodiment is shown in fig. 1 to 3, and comprises an oxidation coagulation reaction tank 1, a composite multiphase separator 2, a denitrification reactor 3, a wall breaking reaction tank 4, a ceramic membrane reactor 5, a sludge concentration tank 6, a filter press 7, a first agent adding system 8, a second agent adding system 9, a third agent adding system 10 and a fourth agent adding system 11. The above parts can be communicated through pipelines, and valves and pumps are arranged on the pipelines. The first medicament adding system 8, the second medicament adding system 9, the third medicament adding system 10 and the fourth medicament adding system 11 respectively comprise a storage tank 12 for storing medicaments, a pipeline connected with the storage tank 12 and a pump arranged on the pipeline.
The oxidation coagulation reaction tank 1 is provided with a water inlet and a water outlet, sewage to be treated is introduced into the oxidation coagulation reaction tank 1 from the water inlet, and the first agent adding system 8 is communicated with the oxidation coagulation reaction tank 1, in the embodiment, the first agent adding system 8 comprises 3 storage tanks 12 for storing different agents, and respectively stores a pre-oxidant, a ferrous salt aqueous solution and a ferric salt aqueous solution, wherein the pre-oxidant is one or more of potassium permanganate, sodium hypochlorite, ozone and calcium dioxide, the ferrous salt is ferrous sulfate and/or ferrous chloride, and the ferric salt is one or more of ferric sulfate, ferric chloride, polymeric ferric chloride and polymeric ferric sulfate.
After sewage to be treated is treated by a pre-oxidant, a ferrous salt aqueous solution and a ferric salt aqueous solution in an oxidation coagulation reaction tank 1, a water outlet of the auto-oxidation coagulation reaction tank 1 enters a composite multiphase separator 2 through a pipeline, wherein the pipeline connecting the oxidation coagulation reaction tank 1 and the composite multiphase separator 2 is named as a first pipeline. Second medicament dosing system 9 is linked together with first pipeline, and in this embodiment, second medicament dosing system 9 includes 2 storage tanks 12 that are used for storing different flocculating agents, stores polyaluminium chloride (PAC) and Polyacrylamide (PAM) respectively.
The first pipeline is provided with a mixer 13, and the mixer 13 is positioned at the downstream of the connection part of the second medicament adding system 9 and the first pipeline and is used for mixing effluent from the oxidation coagulation reaction tank 1 with a flocculating agent.
As shown in fig. 2, the composite multiphase separator 2 includes a barrel 21, a cyclone 22 disposed at a lower portion of the barrel 21, a baffle plate 23 disposed in the barrel 21 and above the cyclone 22, a sludge concentrating member 24 disposed between the barrel 21 and the cyclone 22, a plurality of inclined plates 25 disposed in the barrel 21 and above the baffle plate 23, and a packing region 26 disposed in the barrel 21 and above the plurality of inclined plates 25, wherein a water inlet of the composite multiphase separator 2 is opened at a side portion of the cyclone 22, a first pipeline is communicated with a water inlet of the composite multiphase separator 2, a water outlet is opened at a top portion of the barrel 21, and a sludge discharge port is opened at bottom portions of the cyclone 22 and the barrel 21. The sludge concentration part 24 comprises a stirrer, and the sludge is slowly stirred by the stirrer and is concentrated and compressed by a gravity concentration method; the inclined plates 25 are arranged in parallel and the extending direction of the inclined plates is intersected with the axial direction of the cylinder 21; the filler filled in the filler area 26 is one or more of hydroxyl iron oxide, activated alumina, zeolite, manganese oxide, iron-manganese composite oxide and ion exchange resin; the particle size range of the filler is 1-2 mm.
The water outlet of the composite multiphase separator 2 is communicated with the denitrification reactor 3, the sludge discharge port of the composite multiphase separator 2 is communicated with the wall breaking reaction tank 4, and a pipeline for communicating the sludge discharge port of the composite multiphase separator 2 with the wall breaking reaction tank 4 is named as a second pipeline. The third chemical adding system 10 is communicated with the second pipeline, in this embodiment, the third chemical adding system 10 includes 1 storage tank 12 for storing an oxidant, and the oxidant is one or more mixed solution of chlorine, chlorine dioxide, hydrogen peroxide and ozone.
The algae-containing sludge and sludge water from the composite multiphase separator 2 and the oxidant are mixed and then enter a wall-breaking reaction tank 4, as shown in fig. 3, the wall-breaking reaction tank 4 comprises an ultraviolet region 41, an ultraviolet-ultrasonic synergistic region 42 and an ultrasonic region 43 which are sequentially arranged from an inlet to an outlet, and the volume ratio of the ultraviolet region 41 to the ultraviolet-ultrasonic synergistic region 42 to the ultrasonic region 43 is 10-25: 2-5: 1. Ultraviolet lamps 44 are arranged in the ultraviolet region 41 and the ultraviolet-ultrasonic cooperation region 42, the length direction of lamp tubes of the ultraviolet lamps 44 is perpendicular to the water flow direction, and the distance between every two adjacent ultraviolet lamps 44 is 2-10 cm. The lower parts of the ultraviolet-ultrasonic cooperative area 42 and the ultrasonic area 43 are provided with an ultrasonic generator 45, and the direction of ultrasonic waves emitted by the ultrasonic generator 45 is perpendicular to the water flow direction.
The outlet of the wall breaking reaction tank 4 is communicated with a ceramic membrane reactor 5, and the ceramic membrane adopted by the ceramic membrane reactor 5 is a microfiltration membrane with the membrane aperture of 0.05-0.45 microns or an ultrafiltration membrane with the interception capability of 50-300 Kda. The water outlet of the ceramic membrane reactor 5 is communicated with the denitrification reactor 3; the concentrated water outlet of the ceramic membrane reactor 5 is communicated with the sludge concentration tank 6, and a pipeline communicating the concentrated water outlet of the ceramic membrane reactor 5 with the sludge concentration tank 6 is named as a third pipeline. The fourth chemical dosing system 11 is communicated with the third pipeline, and in this embodiment, the fourth chemical dosing system 11 includes 2 storage tanks 12 for storing different flocculants, and respectively stores polyaluminium chloride (PAC) and Polyacrylamide (PAM).
The mixture of the concentrated water from the ceramic membrane reactor 5 and the flocculating agent is introduced into a sludge concentration tank 6 for sludge concentration, the water outlet of the sludge concentration tank 6 is communicated with a denitrification reactor 3, the sludge discharge port of the sludge concentration tank 6 is communicated with a filter press 7, the water outlet of the filter press 7 is communicated with the denitrification reactor 3, and filter press sludge cakes discharged from the filter press 7 are safely buried.
The filter press 7 is a belt filter press or a plate and frame filter press. The denitrification reactor 3 is an upflow anaerobic sludge blanket, an internal circulation anaerobic reactor, an anaerobic folded plate reactor or an anaerobic filtration blanket reactor.
Example 1
The algae density of the sewage to be treated is 3.5 multiplied by 107The nitrate nitrogen content is 5.21mg/L, and the COD content is 85 mg/L.
The treatment system is used for treating the sewage to be treated, and the treatment method of the embodiment comprises the following steps:
(1) introducing the sewage to be treated into an oxidation coagulation reaction tank 1, and oxidizing and coagulating the sewage to be treated to remove algae by adding a medicament; wherein the added pre-oxidant is potassium permanganate, and the dosage of the pre-oxidant is that the ratio of the pre-oxidant to the algae cells is 0.5 multiplied by 103mg preoxidant: 0.1X 109Individual algal cells; adding a ferrous sulfate aqueous solution 10min after the pre-oxidant is added, wherein the dosage of the ferrous salt is that the ratio of the ferrous salt to the algae cells is 2mg of the ferrous salt: 0.25X 109Individual algal cells; adding the aqueous solution of ferric sulfate 3min after adding the aqueous solution of ferrous salt, wherein the molar ratio of the ferric salt to the ferrous salt is 0.5: 1; and (3) after the ferric salt is added for 15min, discharging the reaction liquid out of the oxidation coagulation reaction tank 1.
(2) And adding a flocculating agent into the first pipeline, wherein the flocculating agent is polyaluminium chloride and polyacrylamide, the feeding amount of the polyaluminium chloride is 20mg/L, and the feeding amount of the polyacrylamide is 0.5 mg/L.
(3) The filler in the composite multiphase separator 2 is ferric oxyhydroxide solid filler with the particle size range of 1-2 mm, and the retention time of the mixture of the flocculating agent and the sewage in the composite multiphase separator 2 is controlled to be 35 min.
(4) The effluent of the composite multiphase separator 2 is introduced into a denitrification reactor 3, the denitrification reactor 3 is an internal circulation anaerobic reactor, and the retention time of the water to be treated in the denitrification reactor 3 is controlled to be 3 h.
(5) And adding an oxidant into the second pipeline, wherein the oxidant is ozone, and the adding amount of the oxidant is 100mg/g of algal cell dry solids.
(6) Oxidizing and wall-breaking the mixture of the algae-containing sludge and sludge water and the oxidant in a wall-breaking reaction tank 4, wherein the volume ratio of an ultraviolet region 41, an ultraviolet-ultrasonic synergistic region 42 and an ultrasonic region 43 of the wall-breaking reaction tank 4 is 10:2:1, the distance between two adjacent ultraviolet lamps 44 is 5cm, and the ultraviolet dose is 45mJ/cm2The ultrasonic dose is 60mJ/cm2。
(7) And (3) introducing the sludge water treated by the wall-breaking reaction tank 4 into a ceramic membrane reactor 5 for separation, wherein a ceramic membrane adopted by the ceramic membrane reactor 5 is a microfiltration membrane with the membrane aperture of 0.45 micron, and the effluent of the ceramic membrane reactor 5 is introduced into a denitrification reactor 3.
(8) And adding a flocculating agent into the third pipeline, wherein the flocculating agent is polyaluminium chloride and polyacrylamide, the feeding amount of the polyaluminium chloride is 20mg/L, and the feeding amount of the polyacrylamide is 0.5 mg/L.
(9) The mixture of the concentrated water from the ceramic membrane reactor 5 and the flocculating agent is concentrated in the sludge concentration tank 6, the mixture stays in the sludge concentration tank 6 for 40min, and the clear liquid in the sludge concentration tank 6 is introduced into the denitrification reactor 3.
(10) And (3) introducing the concentrated sludge from the sludge concentration tank 6 into a filter press 7 for filter pressing, wherein the filter press 7 is a belt filter press, the pressure filtrate of the filter press 7 is introduced into the denitrification reactor 3, and the sludge cake is safely buried.
Example 2
Essentially the same as example 1, except that: the quality of the inlet water is different, and the algae density of the sewage to be treated is 5.5 multiplied by 107The nitrate nitrogen content is 5.46mg/L, and the COD content is 95 mg/L.
Example 3
Essentially the same as example 1, except that: the quality of the inlet water is different, and the algae density of the sewage to be treated is 1.9 multiplied by 108The nitrate nitrogen content is 6.21mg/L, and the COD content is 107 mg/L. The ultraviolet dose is improved to 60mJ/cm2The dosage of the ultrasonic wave is70mJ/cm2(ii) a The adding amount of the pre-oxidant potassium permanganate is that the ratio of the pre-oxidant to the algal cells is 1 multiplied by 103mg preoxidant: 0.1X 109Individual algal cells; the dosage of the ferrous salt is that the ratio of the ferrous salt to the algae cells is 4 mg: 0.25X 109Individual algal cells; the mole ratio of ferric salt to ferrous salt is 0.8: 1; the dosage of the polyaluminium chloride is 22mg/L, and the dosage of the polyacrylamide is 0.6 mg/L.
Example 4
Essentially the same as example 1, except that: the algae density of the sewage to be treated is 2.1 multiplied by 10 when the water quality is different8The nitrate nitrogen content is 6.43mg/L, and the COD content is 120 mg/L. The ultraviolet dose is improved to 60mJ/cm2The ultrasonic dose is 70mJ/cm2The adding amount of the pre-oxidant potassium permanganate is that the ratio of the pre-oxidant to the algae cells is 1 multiplied by 103mg preoxidant: 0.1X 109Individual algal cells; the dosage of the ferrous salt is that the ratio of the ferrous salt to the algae cells is 4 mg: 0.25X 109Individual algal cells; the mole ratio of ferric salt to ferrous salt is 0.8: 1; the dosage of the polyaluminium chloride is 22mg/L, and the dosage of the polyacrylamide is 0.6 mg/L.
Example 5
Essentially the same as example 1, except that: the algae density of the sewage to be treated is 1.6 multiplied by 10 when the water quality is different9The nitrate nitrogen content is 7.32mg/L, and the COD content is 127 mg/L. The ultraviolet dose is improved to 70mJ/cm2The ultrasonic dose is 80mJ/cm2The adding amount of the pre-oxidant potassium permanganate is that the ratio of the pre-oxidant to the algae cells is 1.2 multiplied by 103mg preoxidant: 0.1X 109Individual algal cells; the dosage of the ferrous salt is that the ratio of the ferrous salt to the algae cells is 8 mg: 0.25X 109Individual algal cells; the mole ratio of ferric salt to ferrous salt is 0.85: 1; the feeding amount of the polyaluminium chloride is 24mg/L, and the feeding amount of the polyacrylamide is 0.7 mg/L; adding an oxidant into the second pipeline, wherein the oxidant is oxygen and chlorine dioxide, and the adding mass ratio is 1: 1, the dosage of the oxidant is 150mg/g algal cell dry solid.
Example 6
Essentially the same as example 1, except that: the algae density of the sewage to be treated is 2.5 multiplied by 10 when the water quality is different9The nitrate nitrogen content is 7.36mg/L, and the COD content is 132 mg/L. The ultraviolet dose is improved to 70mJ/cm2The ultrasonic dose is 80mJ/cm2The adding amount of the pre-oxidant potassium permanganate is that the ratio of the pre-oxidant to the algae cells is 2 multiplied by 103mg preoxidant: 0.1X 109Individual algal cells; the dosage of the ferrous salt is that the ratio of the ferrous salt to the algae cells is 10 mg: 0.25X 109Individual algal cells; the mole ratio of ferric salt to ferrous salt is 0.9: 1; the feeding amount of the polyaluminium chloride is 25mg/L, and the feeding amount of the polyacrylamide is 0.8 mg/L; adding an oxidant into the second pipeline, wherein the oxidant is ozone and chlorine dioxide, and the adding mass ratio is 1: 1, the dosage of the oxidant is 200mg/g algal cell dry solid.
The utility model discloses well algae density adopts the microscopic examination count method to detect, and nitrate nitrogen adopts national standard phenoldisulfonic acid spectrophotometry to detect, and COD adopts the national standard potassium dichromate method to detect.
The water quality at the water outlet of the composite multiphase separator 2 in each example is shown in table 1, the water quality at the water outlet of the ceramic membrane reactor 5, the sludge concentration tank 6 and the filter press 7 is shown in table 2, the water quality at the water inlet and the water outlet of the denitrification reactor 3 is shown in table 3, and the sludge yield in each example is shown in table 4 by taking one ton of water as an example.
TABLE 1
| Sample numbering | Algal Density (number/L) | NO3 --N(mg/L) | COD(mg/L) |
| |
13 | 5.23 | 74 |
| Example 2 | 11 | 5.35 | 79 |
| Example 3 | 12 | 6.06 | 84 |
| Example 4 | 20 | 6.36 | 89 |
| Example 5 | 14 | 7.24 | 94 |
| Example 6 | 15 | 7.28 | 99 |
TABLE 2
TABLE 3
TABLE 4
| Sample numbering | Mud production (g/t) |
| Example 1 | 22.322 |
| Example 2 | 22.345 |
| Example 3 | 23.536 |
| Example 4 | 24.012 |
| Example 5 | 25.426 |
| Example 6 | 25.539 |
The present invention includes but is not limited to the above embodiments, and those skilled in the art can convert the present invention into more embodiments within the claims.
Claims (10)
1. A water body algal bloom treatment system is characterized in that: comprises an oxidation coagulation reaction tank (1), a composite multiphase separator (2) communicated with the water outlet of the oxidation coagulation reaction tank (1), a denitrification reactor (3) communicated with the water outlet of the composite multiphase separator (2), a wall breaking reaction tank (4) communicated with the sludge discharge port of the composite multiphase separator (2), a ceramic membrane reactor (5) communicated with the outlet of the wall breaking reaction tank (4), a sludge concentration tank (6) communicated with the concentrated water outlet of the ceramic membrane reactor (5), and a filter press (7) communicated with the sludge discharge port of the sludge concentration tank (6), the water outlet of the ceramic membrane reactor (5), the water outlet of the sludge concentration tank (6) and the water outlet of the filter press (7) are respectively connected with the denitrification reactor (3).
2. The water body algal bloom treatment system according to claim 1, wherein: the water body algal bloom treatment system further comprises a first medicament adding system (8) communicated with the oxidation coagulation reaction tank (1), a second medicament adding system (9) communicated with the oxidation coagulation reaction tank (1) and the pipeline of the composite multiphase separator (2), a third medicament adding system (10) communicated with the pipeline of the composite multiphase separator (2) and the wall breaking reaction tank (4), and a fourth medicament adding system (11) communicated with the pipeline of the ceramic membrane reactor (5) and the sludge concentration tank (6).
3. The water body algal bloom treatment system according to claim 2, wherein: the first medicament adding system (8) comprises a plurality of storage tanks (12) for storing different medicaments, the second medicament adding system (9) comprises a plurality of storage tanks (12) for storing different flocculating agents, the third medicament adding system (10) comprises one or more storage tanks (12) for storing an oxidizing agent, and the fourth medicament adding system (11) comprises a plurality of storage tanks (12) for storing different flocculating agents.
4. The water body algal bloom treatment system according to claim 1, wherein: the composite multiphase separator (2) comprises a cylinder (21), a cyclone (22) arranged at the lower part of the cylinder (21), a flow baffle plate (23) arranged in the cylinder (21) and positioned above the cyclone (22), a sludge concentration part (24) arranged between the cylinder (21) and the cyclone (22), a plurality of inclined plates (25) arranged in the cylinder (21) and positioned above the flow baffle plate (23), and a filling area (26) arranged in the cylinder (21) and positioned above the inclined plates (25), the composite multiphase separator (2) is provided with a water inlet at the side part of the cyclone (22), a water outlet at the top part of the cylinder (21) and a sludge discharge port at the bottoms of the cyclone (22) and the cylinder (21).
5. The water body algal bloom treatment system according to claim 1, wherein: the wall-breaking reaction tank (4) comprises an ultraviolet region (41), an ultraviolet-ultrasonic synergistic region (42) and an ultrasonic region (43) which are sequentially arranged from an inlet to an outlet, and the volume ratio of the ultraviolet region (41), the ultraviolet-ultrasonic synergistic region (42) and the ultrasonic region (43) is 10-25: 2-5: 1.
6. The water body algal bloom treatment system according to claim 5, wherein: ultraviolet lamps (44) are arranged in the ultraviolet region (41) and the ultraviolet-ultrasonic synergistic region (42), the length direction of lamp tubes of the ultraviolet lamps (44) is perpendicular to the water flow direction, the distance between every two adjacent ultraviolet lamps (44) is 2-10 cm, and the ultraviolet dose is 40-80 mJ/cm2。
7. The water body algal bloom treatment system according to claim 5, wherein: the ultraviolet-ultrasonic cooperation area (42) and the lower part of the ultrasonic area (43) are provided with an ultrasonic generator (45), the direction of ultrasonic waves emitted by the ultrasonic generator (45) is perpendicular to the water flow direction, and the ultrasonic dose is 50-100 mJ/cm2。
8. The water body algal bloom treatment system according to claim 1, wherein: the ceramic membrane adopted by the ceramic membrane reactor (5) is a microfiltration membrane with the membrane aperture of 0.05-0.45 micrometer or an ultrafiltration membrane with the interception capability of 50-300 Kda.
9. The water body algal bloom treatment system according to claim 1, wherein: the filter press (7) is a belt filter press (7) or a plate and frame filter press (7).
10. The water body algal bloom treatment system according to claim 1, wherein: the denitrification reactor (3) is an upflow anaerobic sludge blanket, an internal circulation anaerobic reactor, an anaerobic folded plate reactor or an anaerobic filtration blanket reactor.
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