CN216764640U - Red mud leachate biochemical treatment system - Google Patents
Red mud leachate biochemical treatment system Download PDFInfo
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- CN216764640U CN216764640U CN202220279385.XU CN202220279385U CN216764640U CN 216764640 U CN216764640 U CN 216764640U CN 202220279385 U CN202220279385 U CN 202220279385U CN 216764640 U CN216764640 U CN 216764640U
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Abstract
The utility model discloses a red mud leachate biochemical treatment system, which comprises a solid-liquid separation unit, a high-salt biochemical reaction unit, an ozone catalytic oxidation tower, an SBAF biological aeration filter tank, a single-valve filter and a clear water tank, wherein the solid-liquid separation unit is used for separating activated sludge, the ozone catalytic oxidation tower is used for oxidizing and degrading high-molecular organic matters, the SBAF biological aeration filter tank is used for degrading organic matters and intercepting suspended solids, the single-valve filter is used for filtering, the clear water tank is used for storing treated clear water, and the sludge treatment unit is used for treating sludge separated by the solid-liquid separation unit and the high-salt biochemical reaction unit. The red mud leachate treated by the method has high reaction efficiency and stable treatment effect, can effectively remove COD, F, ammonia nitrogen, TP and sulfide in the red mud leachate wastewater, meets the requirement of surface IV-class water quality at a high standard, greatly reduces the treatment cost and reduces the generation amount of medicament sludge.
Description
Technical Field
The utility model belongs to the technical field of wastewater treatment, and particularly relates to a red mud leachate biochemical treatment system.
Background
With the annual increase of alumina output and gradual reduction of bauxite positions in China, industrial solid waste discharged during alumina extraction in the aluminum production industry is continuously increased in annual production amount of red mud solid waste, a large amount of red mud yards can be generated due to the concentrated stacking of the red mud solid waste, and meanwhile, a large amount of high-salinity leachate wastewater is generated from the red mud yards, so that the waste of land resources, environmental pollution and potential safety hazards are caused, and the industrial solid waste is the focus of attention of governments and people. Meanwhile, with the comprehensive and deep implementation of environmental policies and measures such as national qi ten, water ten, soil ten, and Yangtze river protection, restoration, attack and hardness combat action plan, the comprehensive utilization and proper management of red mud become an environmental protection shackle which is urgently and must be solved by the aluminum refining industry.
While the traditional red mud leachate wastewater treatment with high organic matter concentration mainly adopts a fenton chemical method for treatment, 98% concentrated sulfuric acid, ferrous sulfate, 27.5% hydrogen peroxide, 32% caustic soda, PAC and PAM-are required to be sequentially used for treating IV-class water quality on the ground surface, the treatment cost only reaches 30 yuan/t wastewater, and the production amount of chemical sludge only reaches 0.2m3And/t waste water, and ammonia nitrogen, fluoride and sulfide cannot be effectively treated. Therefore, it is very necessary to provide a biochemical treatment system and a biochemical treatment method for red mud leachate.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a red mud leachate biochemical treatment system and a red mud leachate biochemical treatment method, so that red mud leachate wastewater can be treated to surface IV-class water quality in a high standard manner, ammonia nitrogen, fluoride and sulfide can be effectively treated, and the treatment cost is reduced.
In order to solve the technical problems, the utility model adopts the technical scheme that:
the red mud leachate biochemical treatment system comprises a solid-liquid separation unit, a high-salt biochemical reaction unit, an ozone catalytic oxidation tower, an SBAF biological aeration filter tank, a single-valve filter and a clear water tank, wherein the solid-liquid separation unit, the high-salt biochemical reaction unit, the ozone catalytic oxidation tower, the SBAF biological aeration filter tank, the single-valve filter and the clear water tank are sequentially arranged and are used for sequentially treating leachate, the high-salt biochemical reaction unit is used for separating activated sludge, the ozone catalytic oxidation tower is used for oxidizing and degrading high-molecular organic matters, the SBAF biological aeration filter tank is used for degrading organic matters and intercepting suspended solids, the clear water tank is used for storing treated clear water, and the sludge treatment unit is used for treating sludge separated by the solid-liquid separation unit and the high-salt biochemical reaction unit.
Further, the solid-liquid separation unit comprises a pretreatment comprehensive regulation and control tank for receiving the leachate and performing mixing and stirring regulation and control on the leachate, a desulfurization tank capable of adding polymeric ferrous sulfate to perform fully mixed reaction with sulfide in the leachate, a solid-liquid separation device capable of adding polymeric aluminum chloride to perform reaction with anionic polyacrylamide and separating sludge containing heavy metals and sulfur, and a neutralization tank for receiving the leachate after separating sludge and adding concentrated sulfuric acid to adjust the pH value, the sludge separated by the solid-liquid separation device is discharged into the sludge treatment unit, and the leachate in the neutralization tank is discharged into the high-salinity biochemical reaction unit.
Further, be equipped with first rabbling mechanism and a plurality of corridor formula baffle in the regulation and control pond is synthesized in preliminary treatment.
Preferably, the first stirring mechanism adopts a QJB type submersible stirrer.
Further, the desulfurization pond includes stirring pond and lifting pond, the stirring pond disposes second rabbling mechanism and is used for throwing the first medicine mechanism of throwing polymerization ferrous sulfate, the lifting pond disposes and is used for promoting the filtration liquid to the first elevator pump of solid-liquid separation equipment.
Preferably, the first dosing mechanism has a volume of 2m3The PE dosing barrel and the GM type mechanical diaphragm dosing metering pump.
Further, solid-liquid separation equipment includes that the medicament mixes reaction zone, air water mixing area, settling zone, bagger district, the mixed reaction zone of medicament disposes the second that is used for throwing polyaluminium chloride and anion polyacrylamide and adds medicine mechanism, the air water mixing area disposes air compressor machine, dissolved air pump and third rabbling mechanism, the settling zone disposes the mud scraper, the bagger district is collected mud and is gone into the sludge treatment unit.
Further, the neutralization tank is provided with a third dosing mechanism for dosing concentrated sulfuric acid, a fourth stirring mechanism for stirring and a pH value detection mechanism for detecting pH value.
Preferably, the fourth stirring mechanism adopts a microporous aeration pipe, and the microporous aeration pipe is connected with a neutralization pond aeration device.
Furthermore, the high-salinity biochemical reaction unit comprises an active sludge culture pond capable of adding salt-tolerant strains to promote the growth of active sludge in the percolate, a biological strengthening pond for mixing and stirring the active sludge and the percolate, a hydrolysis acidification pond capable of decomposing macromolecular organic matters into micromolecular organic matters, and an SBR reaction pond for biologically degrading and precipitating and separating the active sludge, wherein the active sludge precipitated and separated in the SBR reaction pond is discharged into the sludge treatment unit and can flow back to the biological strengthening pond, and supernatant is discharged into the ozone catalytic oxidation tower.
Furthermore, the activated sludge culture pond is provided with a folded plate film-hanging type microbial reaction bed, a fourth dosing mechanism for dosing salt-tolerant strains and metering the dosing amount and an automatic strain detection mechanism.
Preferably, the fourth dosing mechanism adopts a metering channel.
Furthermore, the biological strengthening tank is provided with a fifth stirring mechanism, and the fifth stirring mechanism adopts a submersible stirrer.
Further, the hydrolysis acidification tank comprises a filler tank and a secondary sedimentation tank, wherein 80% of suspended composite filler with a film forming ratio is filled in the filler tank, and the secondary sedimentation tank is provided with a second lifting pump for lifting the leachate after hydrolysis acidification to the SBR reaction tank.
Furthermore, the SBR reaction tank is provided with a decanter, an aeration mechanism and a reflux pump for discharging sludge and refluxing sludge.
Preferably, the water decanter adopts a rotary water decanter with the water decanting height of 1.5m, and the aeration mechanism adopts a BK series Roots aeration fan.
Furthermore, a first intermediate water tank for receiving the leachate treated by the high-salt biochemical reaction unit is further arranged between the high-salt biochemical reaction unit and the ozone catalytic oxidation tower, and the first intermediate water tank is provided with a third lifting pump for lifting the leachate to the ozone catalytic oxidation tower.
Further, the ozone catalytic oxidation tower comprises an ozone aeration gas distribution area, a catalyst layer and a contact oxidation area, the ozone aeration gas distribution area is provided with an ozone aeration gas distribution device, and the contact oxidation area is provided with a tail gas return pipe for returning tail gas after catalytic oxidation to the ozone aeration gas distribution device.
Further, the ozone aeration gas distribution device comprises an ozone dissolved gas releaser and an ozone gas distribution pipe, and the ozone gas distribution pipe is arranged at the bottom of the catalyst layer.
Furthermore, the catalyst layer comprises a manganese cobalt catalyst layer and an alumina packing layer which are arranged up and down, and a water buffering area is arranged between the manganese cobalt catalyst layer and the alumina packing layer.
Preferably, the thickness of the manganese cobalt catalyst layer is 1200mm, and the thickness of the alumina filler layer is 800 mm.
Furthermore, a support, a biological stable reaction bed and a filter material layer are arranged in the SBAF biological aeration filter tank, an aeration pipe is arranged in the filter material layer, and an aeration device connected with the aeration pipe is configured.
Furthermore, the thickness of the filter material layer is between 2.5m and 3.5m, and the filter material layer comprises an upper aerobic zone and a lower anoxic zone.
Furthermore, the SBAF biological aerated filter is also provided with a backwashing pipe and a sludge discharge pipe, and the sludge discharge pipe is communicated to the solid-liquid separation unit.
And the second intermediate water tank is arranged between the SBAF biological aerated filter and the single-valve filter and provides a water source required by backwashing for the SBAF biological aerated filter and the single-valve filter.
And the backwashing water collecting tank is used for receiving backwashing water obtained after the SBAF biological aerated filter and the single-valve filter are backwashed, and the backwashing water collected by the backwashing water collecting tank can be discharged into the solid-liquid separation unit for circular treatment.
Furthermore, the sludge treatment unit comprises a sludge collecting tank for receiving the sludge separated by the solid-liquid separation unit and the high-salt biochemical reaction unit, a belt concentrator for concentrating the sludge and reducing the water content, a sludge conditioning tank for condensing, dehydrating and conditioning the concentrated sludge and a plate-and-frame filter press for performing filter pressing treatment on the conditioned sludge.
Further: the sludge collection tank is provided with a sixth stirring mechanism and a fourth lift pump for conveying sludge to the belt thickener.
Preferably, the fourth lift pump is a QJB submersible pump.
Further: the sludge conditioning tank is provided with a fifth dosing mechanism for dosing polyaluminium chloride and cationic polyacrylamide, a seventh stirring mechanism for stirring and a fifth lifting pump for conveying sludge to the plate-and-frame filter press.
Preferably, the fifth lift pump is a screw pump.
Further: the plate and frame filter press is provided with a fifth lift pump for discharging the filtered filtrate into the solid-liquid separation unit.
The utility model has the following beneficial effects:
1. the leachate is treated by the solid-liquid separation unit, the high-salt biochemical reaction unit, the ozone catalytic oxidation tower and the SBAF biological aerated filter in sequence, the reaction efficiency is high, the treatment effect is stable, and COD, F, ammonia nitrogen, TP and sulfide in the red mud leachate wastewater can be effectively removed; the separated sludge is treated in a centralized way by the sludge treatment unit, which is also beneficial to preventing the environment from being polluted.
2. The leachate after catalytic oxidation by ozone is continuously degraded and deeply treated by the SBAF biological aerated filter, the biological oxidation and the interception of suspended solids are integrated, the functions of degrading organic matters, denitrifying and dephosphorizing are realized, the organic matters can be effectively degraded, SS, COD, BOD, NH3-N and TP are removed, and the suspended solids formed after degradation can be filtered and intercepted so as to be convenient for discharge.
3. The indexes of the treated wastewater can be reduced to: COD is less than or equal to 30mg/L, ammonia nitrogen is less than or equal to 1.5mg/L, TP is less than or equal to 0.3mg/L, fluoride is less than or equal to 1.5mg/L, and the high standard meets the requirement of surface IV-class water quality.
4. By adopting the treatment system and the treatment method, the treatment cost can be greatly reduced, and the generation amount of medicament sludge can be reduced.
Drawings
FIG. 1 is a diagram of a system architecture according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a solid-liquid separation unit in an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a high-salt biochemical reaction unit according to an embodiment of the present invention;
FIG. 4 is a schematic structural diagram of an ozone catalytic oxidation tower in an embodiment of the present invention;
FIG. 5 is a schematic structural view of a sludge treatment unit according to an embodiment of the present invention;
FIG. 6 is a process flow diagram of an embodiment of the utility model.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, embodiments of the present invention will be described in detail below with reference to the accompanying drawings. However, it will be appreciated by those of ordinary skill in the art that numerous technical details are set forth in order to provide a better understanding of the present application in various embodiments of the present invention. However, the technical solution claimed in the present application can be implemented without these technical details and various changes and modifications based on the following embodiments. The following embodiments are divided for convenience of description, and should not constitute any limitation to the specific implementation manner of the present invention, and the embodiments may be mutually incorporated and referred to without contradiction.
The utility model is further described with reference to the following figures and specific examples.
Referring to fig. 1, in one embodiment, the red mud leachate biochemical treatment system of the present invention includes a solid-liquid separation unit 100, a high-salt biochemical reaction unit 200 for separating activated sludge, an ozone catalytic oxidation tower 300 for oxidizing and degrading high molecular organic matters, an SBAF biological aerated filter 400 for degrading organic matters and intercepting suspended solids, a single-valve filter 500, and a clean water tank 600 for storing treated clean water, which are sequentially disposed and sequentially treated, and further includes a sludge treatment unit 700 for treating sludge separated by the solid-liquid separation unit 100 and the high-salt biochemical reaction unit 200.
When high-salt leachate in a red mud yard is treated, the leachate is subjected to primary treatment and solid-liquid separation through the solid-liquid separation unit 100, the separated sludge is discharged into the sludge treatment unit 700, the leachate is continuously discharged into the high-salt biochemical reaction unit 200 to perform biochemical reaction, activated sludge is further separated through the biochemical reaction, and the activated sludge after treatment is also discharged into the sludge treatment unit 700 to be uniformly treated.
The leachate treated by the high-salt biochemical reaction unit 200 continuously enters the ozone catalytic oxidation tower 300, and is catalyzed and oxidized by ozone, so as to oxidize and degrade high-molecular organic matters, and B/C is increased due to oxidation of soluble iron and high-molecular organic matters in water by ozone, therefore, the SBAF biological aerated filter 400 is also arranged to continuously degrade and deeply treat the leachate after the ozone catalytic oxidation, the SBAF biological aerated filter 400 integrates biological oxidation and suspended solid interception, has the functions of degrading the organic matters, denitrifying and dephosphorizing, can effectively degrade the organic matters, remove SS, COD, BOD, NH3-N and TP, and can filter and intercept the suspended solid formed after degradation so as to be discharged.
The leachate is treated by a solid-liquid separation unit 100, a high-salt biochemical reaction unit 200, an ozone catalytic oxidation tower 300 and an SBAF biological aeration filter 400, so that COD, F, ammonia nitrogen, TP and sulfide in the leachate can be effectively removed; wherein, each index of the treated wastewater can be reduced to: COD is less than or equal to 30mg/L, ammonia nitrogen is less than or equal to 1.5mg/L, TP is less than or equal to 0.3mg/L, and fluoride is less than or equal to 1.5 mg/L. After being filtered by the single-valve filter 500, the waste water can be discharged into a clean water tank 600 for storage and unified discharge; and the separated sludge is treated in a centralized way by the sludge treatment unit 700, so that the environment pollution can be effectively prevented.
Referring to fig. 2, in some embodiments, the solid-liquid separation unit 100 includes a pretreatment comprehensive regulation and control tank 110 for receiving leachate and performing mixing and stirring regulation and control on the leachate, a desulfurization tank 120 capable of adding polymeric ferrous sulfate to perform a fully mixed reaction with sulfides in the leachate, a solid-liquid separation device 130 capable of adding polymeric aluminum chloride to perform a reaction with anionic polyacrylamide and separating sludge containing heavy metals and sulfur, and a neutralization tank 140 for receiving the leachate after separating sludge and adding concentrated sulfuric acid to adjust ph, wherein the sludge separated by the solid-liquid separation device 130 is discharged into the sludge treatment unit 700, and the leachate in the neutralization tank 140 is discharged into the high-salt biochemical reaction unit 200.
In this embodiment, the pretreatment integrated control tank 110 receives the leachate, and performs sufficient mixing and stirring, then the leachate after mixing and stirring is discharged into the desulfurization tank 120, and the polymeric ferrous sulfate FeSO 4.7H 2O is added to enable the ferrous sulfate FeSO 4.7H 2O to be sufficiently mixed and reacted with the leachate, and the ferrous sulfate FeSO 4.7H 2O is used as an inorganic polymeric flocculant, so that the coagulation performance is excellent, the precipitation speed is fast, no aqueous phase transfer of iron ions is caused, and the method is non-toxic, harmless, safe and reliable, and can effectively flocculate out most of COD and BOD such as sulfide and heavy metal ions in the leachate, thereby achieving the purpose of desulfurization, and facilitating separation through the solid-liquid separation device 130.
The solid-liquid separation device 130 is used for removing heavy metals and sulfur by adding polyaluminium chloride (PAC) and anionic Polyacrylamide (PAM) for reaction and utilizing the effects of electric neutralization, adsorption bridging, coprecipitation net capturing and the like of the two chemical agents of PAC and PAM, more than 30% of suspended matters and insoluble organic matters in water can be removed by adopting uniform water quantity and water quality, more than 90% of heavy metal toxicity and more than 20% of organic toxicity are effectively reduced, more than 30% of biochemical load is reduced, so that sludge containing heavy metals and sulfur is separated by discharging precipitates into the sludge treatment unit 700, and the rest leachate is discharged into the neutralization tank 140.
After receiving the leachate after separating the sludge, the neutralization tank 140 adjusts the pH value to 7-10 by adding concentrated sulfuric acid, and then discharges the leachate into the high-salt biochemical reaction unit 200 for biochemical treatment.
In some embodiments, the pretreatment integrated control tank 110 is divided into four compartments from left to right by three gallery type partition plates 112, the size of the middle two compartments is smaller than that of the head compartment and the tail compartment, the first compartment on the left receives percolate, the first stirring mechanism 111 is arranged in the first compartment, the received percolate is fully mixed and stirred by the first stirring mechanism 111 and gradually enters the fourth compartment from left to right, so that hydraulic retention time is prolonged while the percolate is fully mixed and stirred, stability of waste water amount and water quality of percolate is ensured, and effluent of the fourth compartment enters the desulfurization tank 120 for next treatment.
Wherein, the first stirring mechanism 111 preferably adopts a QJB type submersible mixer, so as to facilitate operation, maintenance and overhaul and ensure the working efficiency.
In some embodiments, the desulfurization tank 120 includes a stirring tank 121 and a lifting tank 122, the stirring tank 121 is configured with a second stirring mechanism 123 and a first dosing mechanism for dosing the polymerized ferrous sulfate, so that the polymerized ferrous sulfate FeSO 4.7H 2O is automatically dosed through the first dosing mechanism, the polymerized ferrous sulfate is automatically stirred through the second stirring mechanism 123, and enters the lifting tank 122 after sufficient reaction, and the lifting tank 122 is configured with a first lifting pump 124 for lifting the leachate to the solid-liquid separation device 130. Wherein, the first medicine adding mechanism adopts a volume of 2m3The PE dosing barrel and the GM type mechanical diaphragm dosing metering pump are used for automatically dosing and metering the dosing amount.
In some embodiments, the solid-liquid separation device 130 includes a reagent mixing reaction zone configured with a second dosing mechanism for dosing polyaluminum chloride PAC and anionic polyacrylamide PAM-, a gas-water mixing zone configured with an air compressor, a dissolved air pump, and a third stirring mechanism, a settling zone configured with a sludge scraper, and a hopper zone that collects sludge and discharges into the sludge treatment unit 700. PAC and PAM are added into a medicament mixing reaction zone for primary mixing reaction, air is supplied and dissolved into the air mixing zone through an air machine and a dissolved air pump, the dissolved air ratio of the air is kept between 1:5 and 1:3, the reaction time is 6 to 10min, meanwhile, the mixture is stirred through a third stirring mechanism, so that the medicament and the percolate are fully reacted, then the mixture is discharged into a settling zone for settling, the liquid at the upper part of the settling zone is discharged into a neutralization tank 140, and the sediment is scraped into a mud bucket zone through a mud scraper and finally discharged into a sludge treatment unit 700.
In some embodiments, the neutralization tank 140 is configured with a third dosing mechanism for adding concentrated sulfuric acid, a fourth stirring mechanism for stirring, and a pH detection mechanism for detecting pH value, so as to facilitate adding concentrated sulfuric acid, improve safety, and efficiently and accurately adjust pH value. The fourth stirring mechanism preferably adopts a microporous aeration pipe, the microporous aeration pipe is connected with a neutralization pond aeration device, the microporous aeration pipe is aerated through the neutralization pond aeration device, and gas gushes out through a plurality of micropores on the microporous aeration pipe and turns over in the percolate, so that the effects of stirring and mixing are achieved.
Referring to fig. 3, in some embodiments, the high salinity biochemical reaction unit 200 includes an activated sludge cultivation tank 210 into which salt-tolerant bacteria can be added to promote the growth of activated sludge in leachate, a biological strengthening tank 220 for mixing and stirring activated sludge and leachate, a hydrolysis acidification tank 230 for decomposing macromolecular organic matters into small molecular organic matters, and an SBR reaction tank 240 for biodegradation and precipitation separation of activated sludge, wherein the activated sludge precipitated and separated by the SBR reaction tank 240 is discharged into the sludge treatment unit 700 and can be returned to the biological strengthening tank 220, and supernatant is discharged into the ozone catalytic oxidation tower 300.
Two adjacent water tanks of the high-salinity biochemical reaction unit 200 can be connected by a water passing hole matched gate valve with the saw tooth height of 20mm, so that the water passing amount and the water quality are ensured to be uniform; or the pipeline and the valve are adopted for connection, so that the smooth connection is ensured. Local rivers effect can all be ensured to two kinds of connected modes, if the one-level pond of last one-level is unusual, the accessible time cutting off is connected to guarantee holistic operation smoothness.
In this embodiment, the activated sludge cultivation pool 210 cultivates the microbial flora by adding salt-tolerant strains such as aerobic halotolerant bacteria and nitrohalotolerant bacteria, and supplements a certain amount of nutrient sources such as carbon source, nitrogen source and phosphorus source to ensure that C: n: p is 100:5:1, and forms a stable and efficient microbial flora to enable the activated sludge to gradually develop and grow.
Then, activated sludge reflowing from the SBR reaction tank 240 is added into the biological strengthening tank 220 in a matching manner, so that cultured microbial flora, full-load percolate wastewater and the activated sludge reflowing from the SBR reaction tank 240 are fully mixed and strengthened, the adapted activated sludge is promoted to be effectively mixed with the newly domesticated activated sludge, the activated sludge is supplemented, the sludge age is prolonged, the biological activities of aerobic halotolerant bacteria, nitrohalotolerant bacteria and the like are improved, and the biochemical stability and biochemical effect are ensured again.
The hydrolysis acidification tank 230 decomposes the macromolecular organic matter into bioavailable small molecular organic matter by a hydrolysis acidification method intermediate between the aerobic and anaerobic treatment methods. Finally, activated sludge is precipitated and separated through the SBR process through the SBR reaction tank 240, the activated sludge is discharged into the sludge treatment unit 700 and the biological strengthening tank 220 according to the proportion of 3:1, and supernatant is discharged into the ozone catalytic oxidation tower 300 for continuous treatment.
In some embodiments, the activated sludge cultivation pond 210 is configured with a folded-plate biofilm culturing type microbial reaction bed 211, a fourth dosing mechanism for dosing the salt-tolerant strains and metering the dosing amount, and an automatic strain detection mechanism. The folded plate film-hanging type microbial reaction bed adopts a hanging diameter phi of 200mm, a sheet distance of 60mm and a specific surface area of 2359m2/m3The fiber bundle combined filler membrane adopts a low biofilm formation ratio of 60 percent, provides an excellent biological implantation breeding bed for salt-tolerant and heavy metal-tolerant culture and domestication of salt-tolerant strains, and ensures the biochemical stability and biochemical effect of a back-end system. The fourth dosing mechanism and the automatic strain detection mechanism are convenient for strain feedingAnd (4) releasing and detecting so as to more accurately and efficiently release the strains. Wherein, the fourth dosing mechanism adopts a metering channel.
In some embodiments, the bioaugmentation tank 220 is configured with a fifth agitation mechanism 221 by which the return activated sludge and the incubated activated sludge are thoroughly mixed. Wherein, the fifth stirring mechanism adopts a submersible stirrer and is arranged at the bottom of the biological strengthening pool 220 for stirring.
In some embodiments, the hydrolysis acidification tank 230 includes a filler tank 231 and a secondary sedimentation tank 232, the filler tank 231 is filled with a composite filler 233 suspended at a film-forming ratio of 80%, and the secondary sedimentation tank 232 is configured with a second lift pump 234 for lifting the leachate after hydrolysis acidification to the SBR reaction tank 240. The filling pool 231 hydrolyzes insoluble organic matters in water into soluble organic matters through hydrolytic bacteria and acidifying bacteria, converts macromolecular substances which are difficult to biodegrade into micromolecular substances which are easy to biodegrade, decomposes the macromolecular organic matters into biological utilization micromolecular organic matters under the action of anaerobic bacteria, the composite filling 233 can intercept part of suspended matters, and the second lifting pump 234 in the secondary sedimentation pool 232 can lift leachate which is hydrolyzed and acidified into the SBR reaction pool 240 for continuous treatment.
In some embodiments, the SBR reaction tank 240 is configured with a decanter 241, an aeration mechanism, and a return pump 242 for sludge discharge and sludge return. The SBR reaction tank 240 is aerated intermittently by an aeration mechanism, integrates homogenization, primary sedimentation, biodegradation and secondary sedimentation into a whole, finally, clear water is periodically discharged by a decanter, the clear water enters the ozone catalytic oxidation tower 300 for continuous treatment, and sludge is discharged into the biological strengthening tank 220 and the sludge treatment unit 700 by a reflux pump 242. Wherein, the decanter 241 adopts a rotary decanter with a decanting height of 1.5m, and the aeration mechanism adopts a BK series Roots aeration fan.
Referring to fig. 4, in some embodiments, a first intermediate water tank 310 for receiving the leachate treated by the high salinity biochemical reaction unit 200 is further disposed between the high salinity biochemical reaction unit 200 and the ozone catalytic oxidation tower 300, and the first intermediate water tank 310 is configured with a third lift pump 311 for lifting the leachate to the ozone catalytic oxidation tower 300. The leachate treated by the high-salinity biochemical reaction unit 200 can be stored in the first intermediate water tank 310, and after a certain amount of leachate is stored, the leachate is conveyed to the ozone catalytic oxidation tower 300 by the third lift pump 311 to perform the next catalytic ozonation reaction.
In some embodiments, the catalytic ozonation tower 300 comprises an ozone aeration gas distribution area provided with an ozone aeration gas distribution device, a catalyst layer, and a contact oxidation area provided with a tail gas return pipe for returning the catalytically oxidized tail gas to the ozone aeration gas distribution device.
In the embodiment, ozone O is introduced into the ozone aeration gas distribution area through the ozone aeration gas distribution device3Ozone O3And the leachate treated by the high-salt biochemical reaction unit 200 enters a catalyst layer, is accelerated to react under the action of a catalyst, is discharged into the SBAF biological aerated filter 400 for continuous treatment after stable reaction in a contact oxidation zone, and the reacted ozone tail gas flows back to the ozone aeration gas distribution device for treatment through a tail gas return pipe and continuously generates ozone O3. By ozone O3The catalytic oxidation effect of the catalyst has stronger capabilities of decoloring and removing organic pollutants, so that the high molecular organic matters which are difficult to degrade can be oxidized and degraded.
In this embodiment, the ozone aeration gas distribution device comprises an ozone dissolved gas releaser and an ozone gas distribution pipe, the ozone gas distribution pipe is arranged at the bottom of the catalyst layer so as to release from the bottom and utilize ozone O3To make it automatically pass through the catalyst layer. In addition, the catalyst layer comprises a manganese-cobalt catalyst layer and an alumina packing layer which are arranged up and down, and a water buffering area is arranged between the manganese-cobalt catalyst layer and the alumina packing layer, wherein the thickness of the manganese-cobalt catalyst layer is 1200mm, the thickness of the alumina packing layer is 800mm, and the water buffering area is arranged according to the retention time of liquid entering for 10 min. By arranging two catalyst layers and arranging a water buffering area between the two catalyst layers, ozone O can be effectively added3Oxidation of organic substances。
In some embodiments, the SBAF biological aerated filter 400 is provided with a support, a biological stabilization reaction bed and a filter material layer, wherein the filter material layer is provided with an aeration pipe and an aeration device connected with the aeration pipe. The SBAF biological aerated filter 400 integrates biological oxidation and suspended solid interception, aeration is carried out in the SBAF biological aerated filter 400 through an aeration device and an aeration pipe, a biological stable reaction bed is arranged on a support, a filter material layer is arranged on the biological stable reaction bed, organic matters are continuously degraded on the filter material layer above the biological stable reaction bed and are filtered through the filter material layer, suspended matters generated are continuously intercepted, and filtered liquid is discharged into a single-valve filter 500 to be filtered and then is discharged into a clean water tank 600 to be discharged.
In the embodiment, the thickness of the filter material layer is between 2.5m and 3.5m, and the filter material layer comprises an upper aerobic zone and a lower anoxic zone. The SBAF biological aerated filter 400 is further provided with a backwash pipe and a sludge discharge pipe, wherein the sludge discharge pipe is communicated to the solid-liquid separation unit 100, and the backwash pipe is used for connecting backwash water so as to clean a filter material layer after running for a period of time and intensively discharge the backwash water to the solid-liquid separation unit 100 through the sludge discharge pipe.
In some embodiments, to provide backwash water nearby, a second intermediate water tank 800 is further included between the SBAF bio-aerated filter 400 and the single-valve filter 500, the second intermediate water tank 800 providing a source of water required for backwash to the SBAF bio-aerated filter 400 and the single-valve filter 500.
In addition, the system also comprises a backwash water collecting tank 900 for receiving backwash water after the SBAF biological aerated filter 400 and the single-valve filter 500 are backwashed, and the backwash water collected by the backwash water collecting tank 900 can be discharged into the solid-liquid separation unit 100 for recycling treatment. The second intermediate water tank 800 provides a water source required by backwashing for the SBAF biological aeration filter 400 and the single-valve filter 500, and the sewage after backwashing of the SBAF biological aeration filter 400 and the single-valve filter 500 is uniformly discharged to the backwashing water collection tank 900 and then is intensively discharged to the solid-liquid separation unit 100 for circular treatment.
Referring to fig. 5, in some embodiments, the sludge treatment unit 700 includes a sludge collection tank 710 for receiving the sludge separated by the solid-liquid separation unit 100 and the high-salt biochemical reaction unit 200, a belt thickener 720 for thickening the sludge to reduce the water content, a sludge conditioning tank 730 for coagulation dewatering conditioning the thickened sludge, and a plate and frame filter press 740 for filter-pressing the conditioned sludge. The water content of the sludge is reduced in a gradient manner by adopting a sludge collection → belt concentrator concentration → sludge conditioning → plate and frame filter press filter pressing mode, so that the water content of the sludge can be ensured to be less than or equal to 60%.
In this embodiment, the sludge separated by the solid-liquid separation unit 100 and the high-salt biochemical reaction unit 200 is received by the sludge collection tank 710, and the sludge collection tank 710 is configured with a sixth stirring mechanism 711 and a fourth lift pump 712 for conveying the sludge to the belt concentrator 720, wherein the fourth lift pump 712 adopts a QJB submersible pump. The received sludge is stirred by the fourth lift pump 712 so as to be mixed with the sludge separated twice, and then the sludge is conveyed to the belt thickener 720 by the fourth lift pump 712, concentrated into 90% of sludge moisture content by the belt thickener 720, and then enters the sludge conditioning tank 730 for treatment.
In this embodiment, the sludge conditioning tank 730 is configured with a fifth dosing mechanism for dosing polyaluminium chloride PAC and cationic polyacrylamide PAM +, a seventh stirring mechanism 731 for stirring, and a fifth lift pump 732 for delivering sludge to the plate and frame filter press 740. Wherein, the fifth lift pump 732 is a screw pump. After the sludge conditioning tank 730 receives the concentrated sludge, PAC and PAM + are added through a fifth dosing mechanism, then the sludge is stirred through a seventh stirring mechanism 731, so that a chemical agent and the sludge are fully mixed, the sludge is subjected to condensation dehydration conditioning, finally the conditioned sludge is conveyed to a plate-and-frame filter press 740 through a fifth lifting pump 732, the plate-and-frame filter press 740 is subjected to filter pressing treatment through the dehydration pressure of 1.2MPa-1.6MPa, the moisture content of the sludge is reduced to be below 60%, and finally dry sludge with the moisture content of below 60% is transported outside uniformly.
In order to prevent the filtered filtrate from polluting the environment, the plate-and-frame filter press 740 is provided with a fifth lift pump for discharging the filtered filtrate into the solid-liquid separation unit 100, and the filtrate filtered by the plate-and-frame filter press 740 is discharged into the solid-liquid separation unit 100 through the fifth lift pump for circulation treatment, so as to prevent the filtrate from being polluted.
Referring to fig. 6, a processing method based on the processing system in the foregoing embodiment includes the following steps:
the method comprises the following steps of firstly, treating leachate and separating sludge containing sulfur and heavy metals, and specifically comprises the following substeps:
A1. the leachate is pretreated and comprehensively regulated, and the concentration is controlled according to the following parameters: the content of sulfide is less than or equal to 15mg/L, the content of SS is less than or equal to 300mg/L, and the content of COD is less than or equal to 500 mg/L; by intensively discharging the leachate into the comprehensive pretreatment control tank 110 for comprehensive pretreatment control, parameters of the leachate treated each time can be uniformly adjusted, so that subsequent standardized treatment can be conveniently performed.
A2. Adding polymeric ferrous sulfate for flocculation, and fully mixing and stirring. Discharging the regulated percolate into a desulfurization tank 120, adding 10% polymeric ferrous sulfate FeSO4 & 7H2O, stirring for 15min to fully react, and flocculating out most sulfides, heavy metal ions and other COD and BOD in the percolate.
A3. Separating sludge containing heavy metal ions and sulfur; PAC and anionic polyacrylamide PAM are sequentially added into the solid-liquid separation device 130, and are respectively mixed, stirred and reacted for 6-10min to form uniform alum floc, microbubble dissolved air water with the particle size of 10-20 mu m is introduced, and is fully and effectively mixed and contacted for 30s, the air-water ratio of the microbubble dissolved air water is 1:8, and sludge containing heavy metals and sulfur is separated through the solid-liquid separation device 130 by utilizing the action of the dissolved air with the dissolved air ratio of 1: 5-1: 3.
A4. And (3) pH value blending: and discharging the leachate after the sludge is primarily separated by the solid-liquid separation device 130 into the neutralization tank 140, and adding 98% concentrated sulfuric acid to adjust the pH value of the leachate to 7-10 so as to carry out subsequent biochemical treatment.
Step two, leachate biochemical reaction is carried out, and activated sludge is separated; the method specifically comprises the following substeps:
B1. salt-tolerant strains and nutrient substances are added into the activated sludge culture pond 210, a folded plate biofilm-hanging type microbial reaction bed in the activated sludge culture pond 210 provides an excellent biological implantation propagation bed for salt-tolerant and heavy metal-tolerant culture and domestication of the strains, culture of activated sludge microbial flora is carried out, and a certain amount of wastewater and nutrient sources such as a carbon source, a nitrogen source and a phosphorus source are added in a matching manner, so that C is ensured: n: p is 100:5:1, and forms a stable and efficient microbial flora to enable the activated sludge to gradually develop and grow; and (3) keeping observation and carrying out real-time detection in the cultivation process, ensuring that the colony concentration of the salt-tolerant strain is not more than 25000mg/L and the COD removal efficiency is more than 85%, and then carrying out the next treatment. Wherein the nitrogen source and the phosphorus source can be disodium hydrogen phosphate and urea respectively.
B2. The microbial flora intensively cultured and fully mixed with the full-load percolate in the biological strengthening tank 220 promotes the adapted activated sludge to be effectively mixed with the newly domesticated activated sludge, supplements the activated sludge, prolongs the sludge age, improves the biological activities of aerobic halotolerant bacteria, nitrohalotolerant bacteria and the like, and simultaneously ensures the biochemical stability and biochemical effect again.
B3. In the hydrolysis acidification tank 230, the macromolecular organic matter is decomposed into bioavailable small molecular organic matter by hydrolysis acidification.
B4. Performing biodegradation in the SBR reaction tank 240 through SBR reaction, precipitating and separating activated sludge, and refluxing part of the activated sludge to the step B2 to participate in mixing and strengthening. Wherein the return flow of the activated sludge is 1/4 of the total amount, namely, the activated sludge is discharged into the biological strengthening tank 220 and the sludge treatment unit 700 respectively according to the proportion of 1: 3.
Thirdly, carrying out catalytic oxidation reaction by ozone, and oxidizing and degrading high molecular organic matters; the catalytic ozonation reaction is carried out by an ozone catalytic oxidation tower 300, and the effective volume of a single reaction tower of the ozone catalytic oxidation tower 300 is not less than 77m3The adding concentration of ozone is not less than 48g/h, and ozone O is added3The catalytic oxidation of the catalyst can oxidize and degrade the high molecular organic matters which are difficult to degrade.
Fourthly, the SBAF biological aerated filter 400 is used for further degrading organic matters, denitrifying and dephosphorizing by biological oxidation, and intercepting suspended solids.
Fifthly, the leachate after the treatment is filtered by the single-valve filter 500, so that the leachate is purified into clear water and can be discharged into a clear water tank 600 for discharge
Sixthly, treating the sludge separated in the step A and the step B, and specifically comprising the following substeps:
F1. the sludge separated in the first and second steps is collected by the sludge collecting tank 710 and mixed well.
F2. The sludge is concentrated by a belt concentrator 720, the water content is reduced, the sludge is concentrated to 90% of the sludge water content, and then the sludge is discharged into a sludge conditioning tank 730.
F3. PAC with the concentration of 100mg/L is added into the concentrated sludge according to 10 percent of the total amount of the sludge, and PAM + with the concentration of 5mg/L and the ionic degree of 10-60 is added into the concentrated sludge according to 2 per mill of the total amount of the sludge, so that the sludge is coagulated, dehydrated and conditioned.
F4. Performing filter pressing treatment on the conditioned sludge through a plate and frame filter press 740 to enable the water content of the sludge to be less than 60%, then uniformly transporting the sludge outwards, and returning the filtrate subjected to filter pressing separation to the first step of circular treatment.
By the treatment method, COD, F, ammonia nitrogen, TP and sulfides in the high-salinity leachate of the red mud yard can be effectively removed, effluent can reach COD less than or equal to 30mg/L, fluoride less than or equal to 1.5mg/L, ammonia nitrogen less than or equal to 1.5mg/L, total phosphorus less than or equal to 0.3mg/L and sulfide less than or equal to 0.5mg/L, and heavy metals such as copper, zinc, manganese and the like can be separated, so that the water quality requirement of surface IV-class water is met.
In one embodiment, the red mud leachate containing organic substances, heavy metals, fluorine, sulfur and ammonia nitrogen with the concentration of COD (200 mg/L), ammonia nitrogen (15 mg/L), fluoride (7 mg/L), sulfide (26 mg/L) and water inflow of 150m3/h is treated, wherein:
in the desulfurization stage, the concentration of the polymerized ferrous sulfate FeSO4 & 7H2O added into a desulfurization tank is 10%, and the stirring time is 15 min; in the solid-liquid separation stage, anionic polyacrylamide PAM-with molecular formulas of PAC and 1400w is sequentially added into a solid-liquid separation device 130; the concentration of the salt-tolerant strains added in the activated sludge cultivation stage is 10%, and the ratio of the supplemented carbon source, the supplemented nitrogen source and the supplemented phosphorus source is 100:5: 1. In the sludge treatment stage, the concentration of PAC added into the sludge conditioning tank is 100mg/LPAC, the adding amount is 10% of the total amount of the sludge, the concentration of PAM + added into the sludge conditioning tank is 5mg/L, the ionicity is 10-60, and the adding amount is 2 per mill of the total amount of the sludge.
Finally, the indexes of the clean water discharged into the clean water tank 600 after being filtered by the single-valve filter 500 are as follows:
COD 27.6mg/L, fluoride 1.22mg/L, ammonian 0.98mg/L, total phosphorus 0.25mg/L, sulfide 0.39 mg/L.
The water content of the mud cake after filter pressing by the plate-and-frame filter press is 58 percent.
The treatment cost is reduced to 12 yuan/t of wastewater, the generation amount of medicament sludge is only 10 percent of that of the traditional method, the treatment cost is greatly reduced, and the generation amount of medicament sludge is reduced.
In another embodiment, the red mud leachate containing organic substances, heavy metals, fluorine, sulfur and ammonia nitrogen with the concentration of COD 460mg/L, ammonia nitrogen 41mg/L, fluoride 10mg/L, sulfide 90mg/L and water inflow 200m3/h is treated, wherein:
in the desulfurization stage, the concentration of the polymerized ferrous sulfate FeSO4 & 7H2O added into a desulfurization tank is 10%, and the stirring time is 15 min; in the solid-liquid separation stage, anionic polyacrylamide PAM-with molecular formulas of PAC and 1400w is sequentially added into a solid-liquid separation device 130; the concentration of the salt-tolerant strains added in the activated sludge cultivation stage is 10%, and the ratio of the supplemented carbon source, the supplemented nitrogen source and the supplemented phosphorus source is 100:5: 1. In the sludge treatment stage, the concentration of PAC added into the sludge conditioning tank is 100mg/LPAC, the adding amount is 10% of the total amount of the sludge, the concentration of PAM + added into the sludge conditioning tank is 5mg/L, the ionicity is 10-60, and the adding amount is 2 per mill of the total amount of the sludge.
Finally, the indexes of the clean water discharged into the clean water tank 600 after being filtered by the single-valve filter 500 are as follows:
COD is 28.4mg/L, fluoride is 1.36mg/L, ammonia nitrogen is 1.12mg/L, total phosphorus is 0.23mg/L, and sulfide is 0.44 mg/L.
The water content of the mud cake after filter pressing by the plate-and-frame filter press is 58 percent.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modifications, equivalent variations and modifications made on the above embodiment according to the technical spirit of the present invention are within the scope of the technical solution of the present invention without departing from the technical solution of the present invention.
Claims (9)
1. The red mud leachate biochemical treatment system is characterized by comprising a solid-liquid separation unit (100), a high-salt biochemical reaction unit (200), an ozone catalytic oxidation tower (300), an SBAF biological aeration filter pool (400), a single-valve filter (500) and a clear water pool (600), wherein the solid-liquid separation unit (100) is used for separating activated sludge, the ozone catalytic oxidation tower (300) is used for oxidizing and degrading high-molecular organic matters, the SBAF biological aeration filter pool is used for degrading organic matters and intercepting suspended solids, the single-valve filter is used for filtering, the clear water pool is used for storing treated clear water, and the sludge treatment unit (700) is used for treating sludge separated by the solid-liquid separation unit (100) and the high-salt biochemical reaction unit (200).
2. The red mud leachate biochemical treatment system according to claim 1, wherein the solid-liquid separation unit (100) comprises a pretreatment comprehensive regulation and control tank (110) for receiving leachate and performing mixing and stirring regulation and control on the leachate, a desulfurization tank (120) capable of adding ferrous polysulfate to fully mix and react with sulfides in the leachate, a solid-liquid separation device (130) capable of adding polyaluminium chloride to react with anionic polyacrylamide and separate sludge containing heavy metals and sulfur, and a neutralization tank (140) for receiving the leachate after separating sludge and adding concentrated sulfuric acid to adjust the pH value, wherein the sludge separated by the solid-liquid separation device (130) is discharged into the sludge treatment unit (700), and the leachate in the neutralization tank (140) is discharged into the high-salt biochemical reaction unit (200).
3. The red mud leachate biochemical treatment system according to claim 1, wherein the high salt biochemical reaction unit (200) comprises an activated sludge cultivation tank (210) capable of adding salt-tolerant strains to promote the growth of activated sludge in leachate, a biological strengthening tank (220) for mixing and stirring activated sludge and leachate, a hydrolysis acidification tank (230) capable of decomposing macromolecular organic matters into small molecular organic matters, and an SBR reaction tank (240) for biodegradation and precipitation separation of activated sludge, wherein the activated sludge precipitated and separated by the SBR reaction tank (240) is discharged into the sludge treatment unit (700) and can flow back to the biological strengthening tank (220), and supernatant is discharged into the ozone catalytic oxidation tower (300).
4. The red mud leachate biochemical treatment system according to claim 1, wherein a first intermediate water tank (310) for receiving the leachate treated by the high salinity biochemical reaction unit (200) is further disposed between the high salinity biochemical reaction unit (200) and the ozone catalytic oxidation tower (300), and the first intermediate water tank (310) is configured with a third lift pump (311) for lifting the leachate to the ozone catalytic oxidation tower (300).
5. The biochemical treatment system for red mud leachate according to claim 1, wherein the catalytic ozonation tower (300) comprises an ozone aeration gas distribution area, a catalyst layer and a contact oxidation area, the ozone aeration gas distribution area is provided with an ozone aeration gas distribution device, and the contact oxidation area is provided with a tail gas return pipe for returning tail gas after catalytic oxidation to the ozone aeration gas distribution device.
6. The biochemical treatment system for red mud leachate according to claim 1, wherein a support, a biostable reaction bed and a filter material layer are arranged in the SBAF biological aerated filter (400), and an aeration pipe and an aeration device connected with the aeration pipe are arranged in the filter material layer.
7. The red mud leachate biochemical treatment system of claim 1, further comprising a second intermediate water tank (800) disposed between the SBAF biological aerated filter (400) and the single valve filter (500), wherein the second intermediate water tank (800) provides a water source required for backwashing to the SBAF biological aerated filter (400) and the single valve filter (500).
8. The red mud leachate biochemical treatment system according to claim 7, further comprising a backwashing water collection tank (900) for receiving backwashing water after the SBAF biological aerated filter (400) and the single-valve filter (500) are backwashed, wherein the backwashing water collected by the backwashing water collection tank (900) can be discharged into the solid-liquid separation unit (100) for cyclic treatment.
9. The red mud leachate biochemical treatment system according to claim 1, wherein the sludge treatment unit (700) comprises a sludge collection tank (710) for receiving the sludge separated by the solid-liquid separation unit (100) and the high-salt biochemical reaction unit (200), a belt concentrator (720) for concentrating the sludge to reduce the water content, a sludge conditioning tank (730) for performing coagulation dehydration conditioning on the concentrated sludge, and a plate and frame filter press (740) for performing filter press treatment on the conditioned sludge.
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