CN220183027U - Membrane concentrate full-quantification treatment system for percolate - Google Patents
Membrane concentrate full-quantification treatment system for percolate Download PDFInfo
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a membrane concentrate full-quantification treatment system of percolate, and relates to the technical field of environmental protection. The device comprises a high-grade oxidation device, a salt-resistant biochemical device, a specific moving bed biological film integrated device, a biological aerated filter, a dosing device and a sludge concentration and dehydration system, wherein the high-grade oxidation device, the salt-resistant biochemical device and the specific moving bed biological film integrated device are sequentially connected with the biological aerated filter through pipelines, and the high-grade oxidation device is communicated with the dosing device. The utility model solves the problems of high energy consumption, high operation cost per ton of water and high investment cost of the existing membrane concentrate full-quantization technology, and the system operates in a low energy consumption mode at normal temperature and normal pressure without the problem of concentration and transfer of harmful pollutants, realizes the treatment of the membrane concentrate to reach the emission standard, and avoids the generation of secondary harmful secondary pollutants.
Description
Technical Field
The utility model relates to the technical field of environmental protection, in particular to a membrane concentrate full-quantification treatment system of percolate.
Background
The landfill leachate comprises landfill leachate and incineration plant leachate, and is characterized by high salinity, high ammonia nitrogen, unbalanced carbon nitrogen ratio and extremely poor biodegradability, and the conventional biochemical treatment process is difficult to reach the standard. At present, a biochemical and membrane advanced treatment process is generally adopted for treating percolate, and along with superposition of a plurality of membrane methods, a large amount of membrane concentrate (RO strong brine) cannot be produced and cannot be consumed, so that normal production is affected. The current state puts forward the full quantification treatment requirement of the leachate from the direction of regulation and policy guidance, and the treatment of RO strong brine becomes the problem which needs to be solved for realizing full quantification. The incineration plants generally adopt a back spraying combustion mode to treat the membrane concentrated solution, but the membrane concentrated solution can cause reduction of the heat efficiency of power generation and hearth corrosion; the membrane concentrate is treated by recharging the garbage stack body in garbage landfill, but because of recharging the membrane concentrate for a long time, salt enrichment is formed, so that the quality of the water in the regulating tank is deteriorated, and the stable operation and even the breakdown of the original sewage treatment system are affected. Therefore, urgent demands are made on further treatment of the membrane concentrate of the percolate, the national standard GB16889 clearly proposes that the membrane concentrate cannot be refilled in the updated and revised solicitation opinion in 2021, the risk of illegal environmental protection exceeding the standard is avoided in a short term for avoiding impact breakdown on the original system, and the development of industry technology is guided to be healthier, reliable and practical for a long term.
In recent years, for membrane concentrate treatment of percolate, environmental protection companies and scientific research institutes have proposed several solutions, mainly MVR evaporation technology and submerged combustion technology. The MVR evaporation technology mainly converts electric energy into heat energy to heat high-concentration film concentrated solution, carries out heat exchange evaporation in a strong corrosion resistant evaporator, condenses vapor generated by evaporation, carries out post-treatment to reach the standard, and then discharges the vapor, and the pollutant is concentrated into mother solution; the immersed combustion technology is similar to evaporation in nature, the difference is that the type and energy of the evaporator are different, primary energy is utilized, gas mixture is adopted to burn in water in an immersed mode, heat generated by combustion is directly conducted to enable water in the membrane concentrated solution to evaporate, evaporated condensate water is discharged after one-step treatment after reaching standards, pollutants are further reduced and concentrated into evaporation residues, and compared with MVR evaporation technology, the problem of evaporator scaling is solved, but the treatment of combustion tail gas is increased.
However, the MVR evaporation technique and the submerged combustion technique have the following problems: (1) high equipment investment cost: the membrane concentrate has higher chloride ion content and stronger corrosiveness, and meanwhile, because the concentrated water has higher hardness after the membrane is concentrated, a large amount of acid is needed for pH adjustment to prevent equipment pipeline scaling, the corrosiveness is further enhanced, a titanium alloy material with super-strong corrosion resistance is needed to be adopted as the main body of the evaporator along with the increase of the temperature of the feed liquid, and the material cost is high and the processing is complex; (2) high energy consumption and high operation cost: in principle, evaporation realizes the phase change of water by energy conversion and heat conduction, and a large amount of electric energy is consumed to convert the water into heat energy or the heat generated by combustion of combustible gas is consumed to heat and evaporate the water at normal temperature. The comprehensive cost of treating each ton of membrane concentrate in practical application is about 200 yuan due to the influence of the conductivity of the external heat. (3) The system has strong professionality in operation, is difficult to master by general operators, and is complex in management: the evaporation system belongs to the boiler technology in principle, the control of technological parameters is complex, the professional level requirement on personnel is higher in operation, the percolate belongs to the municipal sanitation field, the management of the urban management department is generally carried out, the skill and the professional level of personnel in first-line operation of sanitation are difficult to reach the professional degree of thermal power plants and chemical plants, and the later-period taking over operation is difficult. (4) incomplete treatment: the evaporation process is not capable of realizing the decomposition of pollutants in principle, the residual high-concentration salt-containing mother solution or crystallized salt is difficult to further process, the method belongs to a fuzzy zone in regulation, and although whether the mother solution is dangerous waste or not is not definitely specified, after the concentration ratio is high, the concentration of part of heavy metal ions in the mother solution reaches the dangerous waste standard, after the concentration, the toxicity is higher, the heavy metal ions exceed the standard and cannot be processed by a conventional method, the treatment is generally carried out according to the dangerous waste price, and the secondary treatment cost is higher. In view of the above, the utility model provides a membrane concentrate full-quantification treatment system for percolate.
Disclosure of Invention
The utility model aims to solve the technical problem of providing a membrane concentrate full-quantification treatment system of percolate. The utility model solves the problems of high energy consumption, high operation cost per ton of water and high investment cost of the prior membrane concentrate (RO strong brine) full quantization technology, and the system is operated in a low energy consumption mode at normal temperature and normal pressure completely, so as to avoid the problem of concentration and transfer of harmful pollutants, realize the treatment of the membrane concentrate to reach the discharge standard, and avoid the generation of secondary harmful secondary pollutants.
The utility model aims to solve the technical problems, and provides a membrane concentrate full-quantification treatment system for percolate, which comprises a high-grade oxidation device, a salt-tolerant biochemical device, a specific moving bed biological membrane integrated device, a biological aerated filter, a dosing device and a sludge concentration system, wherein the high-grade oxidation device, the salt-tolerant biochemical device and the specific moving bed biological membrane integrated device are sequentially connected with the biological aerated filter through pipelines, the high-grade oxidation device is communicated with the dosing device, and the high-grade oxidation device, the salt-tolerant biochemical device and the specific moving bed biological membrane integrated device are respectively connected with the sludge concentration system.
Firstly, the membrane concentrate enters an advanced oxidation device from a membrane concentrate storage tank in a constant quantity through a pump, a reaction reagent is added for catalytic oxidation after pH adjustment, and macromolecular organic matters difficult to degrade are subjected to catalytic oxidation and broken chains to decompose into micromolecular organic matters, so that the biodegradability of wastewater is improved, and part of pollutants are removed. And secondly, discharging the oxidized membrane concentrated solution after the Fenton advanced oxidation device reaction from a coagulating sedimentation area, greatly improving the biodegradability, and enabling the oxidized membrane concentrated solution to enter a salt-tolerant biochemical device for biochemical reaction under the anoxic condition. And then, the effluent (membrane concentrate after anoxic treatment) of the salt-tolerant biochemical device directly flows into a specific moving bed biological membrane integrated device (A/SMBR integrated device), and under the action of a large number of microorganisms, the effluent is discharged to a final-stage biological aerated filter 7 (BAF device) guaranteeing device from a sedimentation zone after anoxic and aerobic alternate reactions, and finally the effluent is discharged up to the standard. Finally, the final-stage guaranteeing device biological aerated filter can realize the guaranteeing and removing effects of total nitrogen and ammonia nitrogen and can play a certain filtering effect.
The beneficial effects of adopting above-mentioned scheme are: the utility model has low equipment investment cost, the total investment of the treatment scale of 100 tons/day of concentrated solution is about 600 ten thousand, the water investment of 6 ten thousand tons, and the equipment cost is reduced by 40 percent compared with the evaporation of 10 ten thousand yuan/ton.
Further, the advanced oxidation device comprises a water inlet adjusting area, a reaction area and a precipitation water outlet area which are sequentially communicated, a water outlet of the precipitation water outlet area is connected with the salt-tolerant biochemical device, and a sludge outlet of the precipitation water outlet area is connected with a sludge concentration system.
Further, the water inlet adjusting area and the reaction area are provided with pneumatic stirring devices.
Further, the inner cavity of the salt-tolerant biochemical device is provided with a filler, the outer wall of the salt-tolerant biochemical device is provided with a circulating pipeline communicated with the inner cavity of the salt-tolerant biochemical device, the circulating pipeline is provided with a circulating water pump, the water outlet of the salt-tolerant biochemical device is connected with the specific moving bed biological film integrated device, and the sludge outlet of the salt-tolerant biochemical device is connected with a sludge concentration system.
Further, the specific moving bed biological membrane integrated device comprises a device bin, an anoxic zone A section and a specific moving bed membrane biological reactor which are sequentially arranged, wherein the device bin is connected with a water outlet of the salt-tolerant biochemical device, the device bin is communicated with the anoxic zone A section, the anoxic zone A section and the specific moving bed membrane biological reactor are connected through a return pipeline, a sludge outlet of the specific moving bed membrane biological reactor is connected with a sludge concentration system, and a water outlet of the specific moving bed membrane biological reactor is connected with the aeration biological filter.
Further, the inner cavity of the anoxic zone A section and the inner cavity of the specific moving bed membrane bioreactor are respectively provided with microorganism carrier fillers.
Further, the biological aerated filter comprises at least two areas of tank bodies, each tank body is sequentially communicated, and ceramic particle fillers are arranged in the inner cavity of each tank body.
Further, a backwash pipeline is arranged in the inner cavity of each tank body, and a backwash water pump is arranged on the backwash pipeline.
Further, the device also comprises a membrane concentrated solution storage tank for receiving and storing the concentrated solution of the membrane system, wherein the membrane concentrated solution storage tank is connected with the advanced oxidation device; the outlet of the sludge concentration system is provided with a plate frame dehydrator, and the water outlet of the plate frame dehydrator is connected with the membrane concentrated solution storage tank.
Further, the device also comprises a PLC automatic control system, wherein the advanced oxidation device, the salt-tolerant biochemical device, the specific moving bed biological membrane integrated device, the biological aerated filter and the dosing device are respectively and electrically connected with the PLC automatic control system.
The utility model also provides a membrane concentrate full-quantification treatment method of the percolate, which comprises the following steps:
(1) Advanced oxidation treatment: performing advanced oxidation treatment on the membrane concentrated solution, treating for 1-4 hours at normal temperature, adjusting the pH to 6-8, adding a flocculating agent, and precipitating to obtain sludge and oxidized membrane concentrated solution;
(2) Salt-tolerant anoxic biochemical treatment: firstly, aerating and activating a composite salt-tolerant strain, then introducing the oxidized membrane concentrate, and carrying out reflux stirring reaction for 1-3 days under the condition of hypoxia and normal temperature to obtain sludge and the membrane concentrate after hypoxia treatment;
(3) Deep biochemical treatment: sequentially carrying out anaerobic and aerobic alternating biochemical treatment on the membrane concentrated solution after anaerobic treatment, carrying out anaerobic biochemical treatment for 1-3 days at normal temperature, carrying out aerobic biochemical treatment for 2-4 days at normal temperature to obtain sludge and membrane concentrated solution after biochemical treatment, and carrying out deep denitrification treatment on the membrane concentrated solution after biochemical treatment to obtain the discharge water reaching the standard.
The advanced oxidation treatment refers to an oxidation treatment technology capable of generating strong oxidative free radicals and utilizing the strong oxidative property of the free radicals to oxidatively decompose organic matters, wherein the oxidation treatment technology comprises Fenton (Fenton) oxidation, ozone catalytic oxidation, electrocatalytic oxidation and the like, and the oxidation reagents adopted by the oxidation are conventional reagents, such as ferrous sulfate and hydrogen peroxide adopted by Fenton (Fenton) oxidation, the concentration of the hydrogen peroxide is 27%, and the mass ratio of the ferrous sulfate to the hydrogen peroxide is 2:1; the advanced oxidation treatment can oxidize, break and break macromolecular organic pollution which is difficult to biochemically degrade in sewage into small molecules, so that biodegradability is improved, or part of pollutants can be directly removed through advanced oxidation. The effluent treated by the step (1) reaches 45-80% of COD and BOD removal rate.
The oxidized membrane concentrated solution is further treated through salt-tolerant biochemical treatment, the biodegradability of the oxidized membrane concentrated solution is improved, the B/C ratio is improved, a nutrient solution is properly added according to water quality (the nutrient solution is purchased from the long technology and comprises a composite carbon source and a microbial accelerant, and the product name code is a micgnonia R101 composite carbon source and a micgnonia R microbial accelerant). The salt-tolerant anoxic biochemical treatment mainly depends on the microbial action of salt-tolerant bacillus, soil bacteria, saccharomycetes and the like on salt, and realizes denitrification and high-efficiency removal of organic matters in a high-salt environment, the ammonia nitrogen removal rate in the step (2) reaches more than 70%, the total nitrogen removal rate reaches more than 60%, the removal rate of COD and BOD reaches 50% -70%, and the conductivity of the effluent after the salt-tolerant anoxic biochemical treatment in the step (2) is reduced by 30% -50% along with the assimilation and absorption of salt-tolerant microbes in the propagation and growth process.
Adopting a specific moving bed biological membrane integrated device (A/SMBR treatment) to treat the obtained membrane concentrate after the anoxic treatment, and adopting a biological aerated filter to achieve the effects of deep denitrification and removal of other organic matters; microbial fillers are added into the anoxic and aerobic biochemical tanks in the step (3), wherein the anoxic section is filled with hollow sphere polyurethane combined filler with the diameter phi of 80-150mm, and the specific surface area of the filler is more than or equal to 300m 2 /m 3 Filling proportion is 30% -60%; the aerobic section is filled with cylindrical HDPE suspended filler with the diameter phi of 10-35mm, the specific surface area of the filler is more than or equal to 500m2/m3, and the filling proportion is 20-50%. And after the suspended filler is added, the membrane is hung, so that the biomass is increased by 60-80% compared with the conventional AO process, and the high-efficiency organic pollutant removing effect is realized. The removal rate of COD and BOD can reach more than 95%, and the denitrification efficiency is higher than 90%. And the membrane concentrate after biochemical treatment is further treated, so that the quality of the final effluent reaches the standard.
In the treatment of the specific moving bed biological membrane integrated device, activated sludge generated by a conventional AO biochemical process of percolate is selected for inoculation, and the concentration of the inoculated sludge is kept within the range of 8000-12000mg/L for operation. The oxygen-deficient zone has the dissolved oxygen content controlled between 0.2 and 0.5mg/L and has the main function of oxygen-deficient denitrification; the aerobic section maintains the content of dissolved oxygen in water at 2-3mg/L through measures such as aeration and the like.
The beneficial effects of the method are that:
(1) Compared with the prior art, the method has the advantage of lower running cost, and is calculated by a 100 ton/day scale membrane concentrated solution treatment system, the ton water energy consumption of the method is only 22Kw h, the electricity price is calculated according to the highest 1 yuan, and the ton water cost is 22 yuan/ton and is only 15% of the evaporation technology; the medicament consumption of ton water is 28 yuan, the labor cost of ton water is 13 yuan, the operation cost is 63 yuan/ton, and the operation cost of ton water of the existing process for fully quantifying the percolate film concentrate is more than 160 yuan.
(2) The utility model thoroughly decomposes pollutants, does not generate transfer, aggregation and concentration of the pollutants, removes all the pollutants through advanced oxidative decomposition and microbial degradation, only generates conventional harmless sludge, can normally return to a landfill after extrusion and dehydration, and does not generate secondary high-concentration secondary pollutants. Different from the evaporation mechanism in the prior art, the method is further concentrated in high power, harmful substances are concentrated and transferred into mother liquor and crystalline salt, the pollution is extremely strong, the concentrated inorganic salt is easy to return to a water body when meeting water, the inorganic salt cannot be buried, the treatment is generally carried out according to the out-of-commission of hazardous waste, and the secondary commission treatment cost is higher.
On the basis of the technical scheme, the utility model can be improved as follows.
Further, in the step (1), the advanced oxidation treatment comprises one or more of Fenton (Fenton) oxidation, ozone catalytic oxidation or electrocatalytic oxidation, preferably the pH of the membrane concentrate is adjusted to 3-5 before the membrane concentrate is subjected to the advanced oxidation treatment by Fenton oxidation; in the step (2), the compound salt-tolerant strain is mainly compounded by salt-tolerant soil bacteria, bacillus and saccharomycetes, the effective viable count in the compound salt-tolerant strain is more than 200 hundred million/g, and the ratio of the effective viable count in the salt-tolerant soil bacteria, the bacillus and the saccharomycetes is (1-5): (3-7): and (1-8), under normal temperature, the microbial inoculum is activated by aeration with water in advance when being added, the aeration activation time of the composite salt-tolerant strain is 0.5-1 day, and the dosage is regulated by a PLC automatic control system according to water source parameters. Wherein the flocculant is polyacrylamide.
Further, the sludge obtained in the steps (1) to (3) is subjected to solid-liquid separation, and the obtained liquid and a mud cake are mixed with the membrane concentrate, and the mud cake is buried.
Drawings
FIG. 1 is a diagram of a full scale treatment system for a percolate membrane concentrate according to the present utility model.
In the drawings, the list of components represented by the various numbers is as follows:
1-a membrane concentrate storage tank; 2-advanced oxidation unit; 3-salt-tolerant biochemical device; 4-a specific moving bed biological membrane integrated device; 5-a dosing device; 6-a sludge concentration system; 7-a biological aerated filter; 8-plate frame dehydrator.
Detailed Description
The principles and features of the present utility model are described below with examples given for the purpose of illustration only and are not intended to limit the scope of the utility model.
Example 1
The embodiment relates to a membrane concentrate full-quantification treatment method of percolate, which comprises the following steps:
(1) Advanced oxidation treatment: performing advanced oxidation treatment on the membrane concentrated solution, treating for 1-4 hours at normal temperature, adjusting the pH to 6-8, adding a flocculating agent, and precipitating to obtain sludge and oxidized membrane concentrated solution;
the advanced oxidation treatment is an oxidation treatment technology capable of generating strong oxidative free radicals and utilizing the strong oxidative property of the free radicals to oxidatively decompose organic matters, and comprises Fenton (Fenton) oxidation, ozone catalytic oxidation, electrocatalytic oxidation and the like, and macromolecule organic pollution which is difficult to biochemically degrade in sewage can be oxidized, broken and broken chains are decomposed into small molecules, so that the biodegradability is improved, or part of pollutants can be directly removed through advanced oxidation.
Preferably, in step (1), the advanced oxidation treatment comprises one or more of Fenton (Fenton) oxidation, ozone catalytic oxidation or electrocatalytic oxidation; the effluent treated by the step (1) reaches 45-80% of COD and BOD removal rate.
(2) Salt-tolerant anoxic biochemical treatment: firstly, aerating and activating a composite salt-tolerant strain, then introducing the oxidized membrane concentrate, and carrying out reflux stirring reaction for 1-3 days under the condition of hypoxia and normal temperature to obtain sludge and the membrane concentrate after hypoxia treatment;
the oxidized membrane concentrated solution is further treated through salt-tolerant biochemical treatment, the biodegradability of the oxidized membrane concentrated solution is improved, the B/C ratio is improved, a nutrient solution is properly added according to water quality (the nutrient solution is purchased from the long technology and comprises a composite carbon source and a microbial accelerant, and the product name code is a micgnonia R101 composite carbon source and a micgnonia R microbial accelerant). The salt-tolerant anoxic biochemical treatment mainly depends on the microbial action of salt-tolerant bacillus, soil bacteria and the like on salt, and realizes denitrification and high-efficiency removal of organic matters in a high-salt environment, the ammonia nitrogen removal rate in the step (2) reaches more than 70%, the total nitrogen removal rate reaches more than 60%, the removal rate of COD and BOD reaches 50% -70%, and the conductivity of the effluent after the salt-tolerant anoxic biochemical treatment in the step (2) is reduced by 30% -50% along with the assimilation and absorption of salt-tolerant microbes in the propagation and growth process.
Preferably, in the step (2), the compound salt-tolerant strain is obtained by compounding salt-tolerant strain powder obtained from the national environmental protection technology of Wuhan water and salt-tolerant soil strain (Bacillus) powder, and the main components of the compound salt-tolerant strain are microbial strains such as salt-tolerant Bacillus, soil strain (Bacillus) and saccharomycetes, wherein the effective viable count in the compound salt-tolerant strain is more than 200 hundred million/gram, and the ratio of the effective viable count in the salt-tolerant soil strain, the Bacillus and the saccharomycetes is (1-5): (3-7): (1-8); the microbial inoculum is activated by water in advance during the addition, and the dosage is adjusted by a PLC automatic control system according to the water source parameters.
(3) Deep biochemical treatment: sequentially carrying out anaerobic and aerobic alternating biochemical treatment on the membrane concentrated solution after anaerobic treatment, carrying out anaerobic biochemical treatment for 1-3 days at normal temperature, carrying out aerobic biochemical treatment for 2-4 days at normal temperature to obtain sludge and membrane concentrated solution after biochemical treatment, and carrying out deep denitrification treatment on the membrane concentrated solution after biochemical treatment to obtain discharge water reaching the standard.
The membrane concentrate after the anoxic treatment is treated by adopting a specific moving bed biological membrane integrated device 4 (A/SMBR integrated treatment), and the effect of removing other organic matters is achieved; microbial fillers are added into the anoxic and aerobic biochemical tanks in the step (3), wherein the anoxic section is filled with hollow sphere polyurethane combined filler with the diameter phi of 80-150mm, and the specific surface area of the filler is more than or equal to 300m 2 /m 3 Filling proportion is 30% -60%; the aerobic section is filled with cylindrical HDPE suspended filler with the diameter phi of 10-35mm, the specific surface area of the filler is more than or equal to 500m2/m3, and the filling proportion is 20-50%. And after the suspended filler is added, the membrane is hung, so that the biomass is increased by 60-80% compared with the conventional AO process, and the high-efficiency organic pollutant removing effect is realized. Can be used forThe removal rate of COD and BOD reaches more than 95%, and the denitrification efficiency is higher than 90%.
And further treating the membrane concentrate after biochemical treatment to ensure that the final effluent quality reaches the standard. A biological aerated filter 7 (BAF device) can be adopted, a cylindrical tower body structure is adopted, ceramic particles are filled in the biological aerated filter, the particle size is 5-10mm, and the porosity is more than 55%. After treatment, organic matters such as COD and the like can be removed to 20% -30%, and the denitrification efficiency is above 30%.
Example 2
The embodiment relates to a full-quantification treatment system for a percolate film concentrated solution, which comprises a high-grade oxidation device 2, a salt-tolerant biochemical device 3, a specific moving bed biological film integrated device 4, a biological aerated filter 7, a dosing device 5 and a sludge concentration system 6, wherein the high-grade oxidation device 2, the salt-tolerant biochemical device 3 and the specific moving bed biological film integrated device 4 are sequentially connected with the biological aerated filter 7 through pipelines, the high-grade oxidation device 2 is communicated with the dosing device 5, and the high-grade oxidation device 2, the salt-tolerant biochemical device 3 and the specific moving bed biological film integrated device 4 (A/SMBR integrated device) are respectively connected with the sludge concentration system 6.
Firstly, the membrane concentrate enters the advanced oxidation device 2 from the membrane concentrate storage tank 1 through a pump constant, after pH adjustment, a reaction reagent is added for catalytic oxidation, and catalytic oxidation and chain breaking are carried out on macromolecular organic matters which are difficult to degrade, so that the membrane concentrate is decomposed into micromolecular organic matters, the biodegradability of wastewater is improved, and meanwhile, part of pollutants are removed.
Preferably, the advanced oxidation device 2 comprises a water inlet adjusting area, a reaction area and a precipitation water outlet area which are sequentially communicated, a water outlet of the precipitation water outlet area is connected with the salt-tolerant biochemical device 3, and a sludge outlet of the precipitation water outlet area is connected with the sludge concentration system 6. The water inlet adjusting area and the reaction area are provided with pneumatic stirring devices.
Specifically, (1) the advanced oxidation device 2 can adopt Fenton method advanced oxidation, is provided with an attached dosing device 5, and the types of the medicaments mainly include acid, alkali, ferrous sulfate, hydrogen peroxide and PAM (polyacrylamide); (2) The Fenton advanced oxidation device 2 adopts an integrated skid-mounted design and comprises a water inlet adjusting area, a reaction area and a precipitation water outlet area, wherein the water inlet adjusting area and the reaction area adopt pneumatic stirring. The integral skid-mounted device integrates key equipment such as a water pump, a fan, an automatic control instrument, a valve and the like and a pipeline system, and the operation of all the equipment is automatically controlled by a PLC; (3) The dosing device 5 matched with the advanced oxidation adopts PLC automatic control, and can automatically adjust dosing amount through on-line instrument feedback of a water inlet adjusting area and a reaction area, thereby realizing accurate dosing.
And secondly, the oxidized membrane concentrated solution after the Fenton advanced oxidation device 2 is reacted is discharged from a coagulating sedimentation area, the biodegradability is greatly improved, and the oxidized membrane concentrated solution enters a salt-tolerant biochemical device 3 to perform biochemical reaction under the anoxic condition.
Preferably, the inner cavity of the salt-tolerant biochemical device 3 is provided with a filler, the outer wall of the salt-tolerant biochemical device 3 is provided with a circulating pipeline communicated with the inner cavity of the salt-tolerant biochemical device 3, the circulating pipeline is provided with a circulating water pump, the water outlet of the salt-tolerant biochemical device 3 is connected with the specific moving bed biological film integrated device 4, and the sludge outlet of the salt-tolerant biochemical device 3 is connected with the sludge concentration system 6.
Specifically, (1) the inside of the salt-tolerant biochemical device 3 is provided with special filler, and the outer wall is provided with a circulating water pump and a pipeline; (2) The salt-resistant biochemical device 3 operates under normal temperature anoxic conditions without heating and mechanical stirring; (3) When in operation, the inner cavity is inoculated with salt-tolerant microorganism strains which are specially domesticated, good biochemistry can be exerted in high-salt wastewater, higher removal efficiency of organic matters such as COD and the like can be achieved, and denitrification effect can be synchronously realized,
and the effluent (membrane concentrate after anoxic treatment) of the salt-tolerant biochemical device 3 directly flows into a specific moving bed biological membrane integrated device 4 (A/SMBR integrated device), and under the action of a large number of microorganisms, the effluent is discharged to a final-stage biological aerated filter 7 (BAF device) guarantee device from a sedimentation zone after anoxic and aerobic alternate reactions, and finally the effluent reaches the standard and is discharged.
Preferably, the specific moving bed biological membrane integrated device 4 comprises a device cabin, an anoxic zone A section and a specific moving bed membrane biological reactor which are sequentially communicated, the device cabin is connected with a water outlet of the salt-tolerant biochemical device 3, the anoxic zone A section is connected with the specific moving bed membrane biological reactor (SMBR device) through a return pipeline, a sludge outlet of the specific moving bed membrane biological reactor is connected with a sludge concentration system 6, and a water outlet of the specific moving bed membrane biological reactor is connected with the biological aerated filter 7. The inner cavity of the anoxic zone A section and the inner cavity of the specific moving bed membrane bioreactor are respectively provided with microorganism carrier fillers.
Specifically, (1) the specific moving bed biological membrane integrated device 4 adopts an integrated design, and the whole equipment is divided into an equipment bin, an anoxic zone A section and a specific moving bed membrane biological reactor aerobic section;
(2) Microbial carrier filler is added into the anoxic zone A and the aerobic zone, and the aerobic zone is provided with a return pipeline to the anoxic zone A; (3) The equipment bin of the specific moving bed biological film integrated device 4 is integrated with a fan, a nutrient solution adding tank, a metering pump, an electric control cabinet, a pipeline valve and the like, a biochemical reaction zone is provided with a PH meter, a DO meter and a sludge concentration meter, and the automatic regulation and automatic sludge discharge of air quantity and dosing quantity are realized under the automatic control of a PLC (programmable logic controller) through the feedback information of an on-line meter.
Finally, the final-stage biological aerated filter 7 guaranteeing device is arranged in at least two areas, so that the guaranteeing and removing effects of total nitrogen and ammonia nitrogen can be realized. The filter tank is composed of a double-section tank body, ceramic particle filler is filled in the tank body, and a certain filtering effect can be achieved.
Preferably, the biological aerated filter 7 comprises at least two areas of tank bodies, each tank body is sequentially communicated, and ceramic particle fillers are arranged in the inner cavity of each tank body. And a backwash pipeline is arranged in the inner cavity of each tank body, and a backwash water pump is arranged on each backwash pipeline.
Specifically, the biological aerated filter 7 guaranteeing device is provided with a backwash water pump and a pipeline, and backwash can be automatically controlled by a PLC.
Preferably, the system further comprises a membrane concentrate storage tank 1, wherein the membrane concentrate storage tank 1 is connected with the advanced oxidation device 2. The outlet of the sludge concentration system 6 is provided with a plate frame dehydrator 8, and the water outlet of the plate frame dehydrator 8 is connected with the membrane concentrated solution storage tank 1. Wherein, the sludge generated by Fenton advanced oxidation and the rear biochemical treatment section is discharged into a sludge concentration system 6, and can be directly treated in a factory after being extruded and dehydrated by a plate frame dehydrator 8, and can be directly backfilled to a landfill site, the incineration factory can return to a garbage storage pit for incineration, no external commission is needed, and the sludge dehydration filtrate is returned to a front concentrated solution storage tank.
Preferably, the system further comprises a PLC automatic control system, wherein the advanced oxidation device 2, the salt-tolerant biochemical device 3, the specific moving bed biological membrane integrated device 4, the biological aerated filter 7 and the dosing device 5 are respectively and electrically connected with the PLC automatic control system.
Test example 1
The project membrane concentrate is treated by a certain leachate in southwest as a sample, the original project leachate treatment process is two stages of AO+UF+DTRO, the water quantity is 300 tons/day, the produced DTRO membrane concentrate is 60 tons/day, and the water quality condition is as follows: cod=4903 mg/L, BOD =1780 mg/L, NH 3-n=417 mg/L, TN =634 mg/L, conductivity=73.5 ms/cm, and national emission standard GB 16889-2008 "pollution control standards for household refuse landfill" table 2 standard corresponding limits are respectively: COD is less than or equal to 100mg/L, BOD is less than or equal to 30mg/L, NH3-N is less than or equal to 25mg/L, TN is less than or equal to 40mg/L, and the effluent has no discharge requirement on conductivity.
This test example treated a membrane concentrate by the following steps:
s1, uniformly conveying the membrane concentrate of the landfill leachate to a pH adjusting area of a high-grade oxidation device 2 in a constant quantity, automatically adjusting the pH to 3-5 according to the inflow rate, and flowing into a reaction area of the high-grade oxidation device 2;
s2, adding ferrous sulfate and hydrogen peroxide into a reaction zone, and simultaneously stirring pneumatically, wherein the concentration of the hydrogen peroxide is 27%, the mass ratio of the ferrous sulfate to the hydrogen peroxide is 2:1, and the reaction time is 120 minutes;
s3, adding caustic soda into an outlet pipeline of the Fenton reaction zone to adjust the pH value to 6-8, then entering a precipitation zone, adding PAM, stirring, flowing into the precipitation zone, and precipitating to obtain effluent COD=2156 mg/L, BOD =816 mg/L, wherein the COD removal rate is 56% and the BOD removal rate is 55%;
s4, discharging Fenton effluent to an intermediate storage pool, conveying the Fenton effluent to a salt-tolerant biochemical device 3 through a lifting pump, adding a composite salt-tolerant strain consisting of salt-tolerant soil bacteria (Bacillus), bacillus, saccharomycetes and the like before starting the salt-tolerant biochemical device 3, enabling the efficient salt-tolerant strain to be subjected to aeration activation for 24 hours, gradually feeding water, adding a composite carbon source nutrient solution, running the salt-tolerant biochemical device 3 at normal temperature, setting external reflux stirring, keeping the reflux ratio to be 100% -300%, keeping the sludge concentration to be 8000mg/L-12000mg/L, and reacting for 1-3 days. After the reaction, the COD of the effluent is less than or equal to 1070mg/L, BOD and less than or equal to 500mg/L, NH < 3 > -N=230 mg/L-165mg/L, TN =250 mg/L-300mg/L.
S5, directly flowing water discharged from the salt-tolerant biochemical device 3 into the A/SMBBR integrated device, sequentially passing through an anoxic zone, an aerobic zone and a precipitation zone, supplementing a carbon source at an inlet according to water quality detection data, wherein the hydraulic retention time HRT=4-6 days, and the water discharged from the precipitation zone after precipitation shows that COD is less than or equal to 91mg/L, BOD and less than or equal to 30mg/L, NH3-N is less than 28mg/L, TN and less than 31mg/L, SS is less than 300mg/L, and all other indexes except SS basically meet the requirements of GB 16889-2008 table 2 discharge standard, so that the BAF guaranteeing device of a treatment section is required to be added to ensure that the water discharged is stable and meets the standard.
S6, treating the effluent of the A/SMBR integrated device by the BAF device, and finally carrying out deep denitrification treatment for 4-6 hours, wherein the detection result of the effluent shows that COD is less than or equal to 71mg/L, BOD and less than or equal to 23mg/L, NH-N is less than 20mg/L, TN and less than 25mg/L, and SS is less than 30mg/L. The effluent meets the discharge standard requirement.
Test example 2
Taking a certain percolate treatment project membrane concentrate in China as a sample, wherein the project main treatment process comprises two stages of AO+UF+NF+RO, and the test water sample is NF+RO membrane concentrate, and the water quality condition is as follows: cod=3790 mg/L, bod=1286 mg/L, NH 3-n=275 mg/L, tn=461 mg/L, conductivity=48 ms/cm.
The water sample of the membrane concentrate is treated according to the flow rate of 200L/h through the following steps:
s1, uniformly conveying the landfill leachate membrane concentrate to a PH adjusting area of a high-level oxidation device 2, adjusting PH to 3-5 according to inflow flow, and flowing into a reaction area of the high-level oxidation device 2;
s2, adding ferrous sulfate and hydrogen peroxide into a reaction zone, and simultaneously carrying out pneumatic stirring, wherein the concentration of the hydrogen peroxide is 27%, the mass ratio of the ferrous sulfate to the hydrogen peroxide is 2:1, and the reaction time is 120 minutes;
s3, adding caustic soda into an outlet pipeline of the Fenton reaction zone to adjust the pH value to 6-8, then entering a precipitation zone, adding PAM, stirring, flowing into the precipitation zone, and precipitating to obtain effluent COD=1753 mg/L, BOD =637 mg/L, wherein the COD removal rate is 46% and the BOD removal rate is 51%;
s4, discharging Fenton effluent to an intermediate storage pool, conveying the Fenton effluent to a salt-tolerant biochemical device 3 through a lifting pump, adding salt-tolerant composite strains before starting the salt-tolerant biochemical device 3, enabling the high-efficiency salt-tolerant strains to be subjected to aeration activation, gradually feeding water, enabling the salt-tolerant biochemical device 3 to operate at normal temperature, and adding composite carbon source nutrient solution at the same time, wherein the reaction time is 2-3 days. After the reaction, the COD of the effluent is not more than 815mg/L, BOD and not more than 309mg/L, NH < 3-N is not more than 130mg/L, TN < 245mg/L.
S5, directly flowing water discharged from the salt-tolerant biochemical device 3 into the A/SMBBR integrated device, sequentially passing through an anoxic zone, an aerobic zone and a precipitation zone, properly supplementing a carbon source at an inlet according to water quality detection data, wherein the hydraulic retention time HRT=4-6 days, and the water discharge test result after precipitation in the precipitation zone shows that COD=69 mg/L, BOD =29 mg/L, NH 3-N=11.5 mg/L, TN =21 mg/L, SS=279 mg/L, and all other indexes basically reach the requirements of GB 16889-2008 table 2 discharge standard except SS, so that the BAF device of a treatment section needs to be increased to ensure that the water discharged stably reaches the standard.
S6, treating the effluent of the A/SMBR integrated device by the BAF guarantee device, and finally carrying out deep denitrification treatment for 4-6 hours, wherein the effluent detection result shows that COD is less than or equal to 58mg/L, BOD and less than or equal to 20mg/L, NH3-N is less than 10mg/L, TN and less than 15mg/L, and SS is less than 30mg/L. All water outlet indexes meet the requirements of GB 16889-2008 table 2 emission standards.
In summary, the utility model has the advantage of lower running cost, and is calculated by a 100 ton/day scale membrane concentrated solution treatment system, the ton water energy consumption of the method is only 22Kw h, the electricity price is calculated according to the highest 1 yuan, and the ton water cost is 22 yuan/ton and is only 15% of the evaporation technology; the medicament consumption of ton water is 28 yuan, the labor cost of ton water is 13 yuan, the operation cost is 63 yuan/ton, and the operation cost of ton water of the existing process for fully quantifying the percolate film concentrate is more than 160 yuan. The utility model thoroughly decomposes pollutants, does not generate transfer, aggregation and concentration of the pollutants, removes all the pollutants through advanced oxidative decomposition and microbial degradation, only generates conventional harmless sludge, can normally return to a landfill after extrusion and dehydration, and does not generate secondary high-concentration secondary pollutants. The utility model has low equipment investment cost, the total investment of the treatment scale of 100 tons/day of concentrated solution is about 600 ten thousand, the water investment of 6 ten thousand tons, and the equipment cost is reduced by 40 percent compared with the evaporation of 10 ten thousand yuan/ton. In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present utility model. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present utility model have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the utility model, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the utility model.
Claims (10)
1. The utility model provides a membrane concentrate full-quantification processing system of percolate, its characterized in that includes advanced oxidation unit (2), salt tolerance biochemical installation (3), specificity remove biological membrane integrated device (4), biological aerated filter (7), dosing device (5) and sludge concentration system (6), advanced oxidation unit (2) salt tolerance biochemical installation (3) reaches specificity remove biological membrane integrated device (4) with biological aerated filter (7) are connected gradually through the pipeline, advanced oxidation unit (2) with dosing device (5) intercommunication, advanced oxidation unit (2) salt tolerance biochemical installation (3) and specificity remove biological membrane integrated device (4) are connected with sludge concentration system (6) respectively.
2. The membrane concentrate full-quantification treatment system of percolate according to claim 1, characterized in that the advanced oxidation device (2) comprises a water inlet adjusting zone, a reaction zone and a precipitation water outlet zone which are sequentially communicated, a water outlet of the precipitation water outlet zone is connected with the salt-tolerant biochemical device (3), and a sludge outlet of the precipitation water outlet zone is connected with the sludge concentration system (6).
3. The membrane concentrate full scale treatment system of percolate according to claim 2, characterized in that said water inlet conditioning zone and said reaction zone are provided with pneumatic stirring means.
4. The membrane concentrate full-quantification treatment system of percolate according to claim 2, characterized in that a filler is arranged in an inner cavity of the salt-tolerant biochemical device (3), a circulating pipeline communicated with the inner cavity of the salt-tolerant biochemical device (3) is arranged on the outer wall of the salt-tolerant biochemical device (3), a circulating water pump is arranged on the circulating pipeline, a water outlet of the salt-tolerant biochemical device (3) is connected with the specific moving bed biological membrane integrated device (4), and a sludge outlet of the salt-tolerant biochemical device (3) is connected with a sludge concentration system (6).
5. The membrane concentrate full-quantification treatment system of percolate according to claim 4, wherein the specific moving bed biological membrane integrated device (4) comprises an anoxic zone A section, a specific moving bed membrane biological reactor and a device bin which are sequentially communicated, the anoxic zone A section is connected with a water outlet of the salt-tolerant biochemical device (3), the anoxic zone A section is connected with the specific moving bed membrane biological reactor through a backflow pipeline, a sludge outlet of the device bin is connected with a sludge concentration system (6), and a water outlet of the device bin is connected with the biological aerated filter (7).
6. The system for the total membrane concentrate quantitative treatment of percolate according to claim 5, wherein the inner cavity of the anoxic zone A section and the inner cavity of the specific moving bed membrane bioreactor are respectively provided with a microbial carrier filler.
7. The membrane concentrate full-quantification treatment system of percolate according to claim 6, wherein the biological aerated filter (7) comprises at least two-zone tanks, each tank is sequentially communicated, and ceramic particle fillers are arranged in the inner cavity of each tank.
8. The membrane concentrate full-scale treatment system of percolate according to claim 7, wherein a backwash pipeline is arranged in each tank body cavity, and a backwash water pump is arranged on the backwash pipeline.
9. The membrane concentrate full-scale treatment system of percolate according to claim 1, characterized by further comprising a membrane concentrate storage tank (1), said membrane concentrate storage tank (1) being connected to the advanced oxidation unit (2); the outlet of the sludge concentration system (6) is provided with a plate frame dehydrator (8), the water outlet of the plate frame dehydrator (8) is connected with the membrane concentrated solution storage tank (1), and the extrusion filtrate returns to the concentrated solution storage tank.
10. The membrane concentrate full-quantification treatment system of percolate according to claim 9, further comprising a PLC automatic control system, wherein the advanced oxidation device (2), the salt-tolerant biochemical device (3), the specific moving bed biological membrane integrated device (4), the biological aerated filter (7) and the dosing device (5) are respectively electrically connected with the PLC automatic control system.
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