WO2021017366A1 - 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置 - Google Patents

基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置 Download PDF

Info

Publication number
WO2021017366A1
WO2021017366A1 PCT/CN2019/124744 CN2019124744W WO2021017366A1 WO 2021017366 A1 WO2021017366 A1 WO 2021017366A1 CN 2019124744 W CN2019124744 W CN 2019124744W WO 2021017366 A1 WO2021017366 A1 WO 2021017366A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
ozone
granular sludge
biofilm
wastewater
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2019/124744
Other languages
English (en)
French (fr)
Inventor
雷利荣
蔡方瑞
李友明
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
South China University of Technology SCUT
Original Assignee
South China University of Technology SCUT
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by South China University of Technology SCUT filed Critical South China University of Technology SCUT
Publication of WO2021017366A1 publication Critical patent/WO2021017366A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/06—Nutrients for stimulating the growth of microorganisms

Definitions

  • the invention relates to the technical field of advanced wastewater treatment, in particular to an advanced wastewater treatment device based on ozone and a biofilm granular sludge reactor.
  • Fenton oxidation technology is currently one of the effective ways to degrade and remove difficult-to-degrade organics in wastewater.
  • ferrous ions catalyze the decomposition of hydrogen peroxide to produce hydroxyl free radicals.
  • organic pollution in the mineralized wastewater Then adjust the pH value of the reaction system to medium or alkaline, iron ions generate iron salt precipitation flocs, and remove organic pollutants, suspended solids and other pollutants in the wastewater through adsorption, coagulation, and precipitation.
  • Fenton oxidation technology has the problems of large amount of chemicals and high treatment cost, and a large amount of iron-containing chemical sludge is produced during the treatment process, which becomes an obstacle to the further promotion and application of Fenton oxidation technology.
  • non-process ions are another obstacle to the recycling of industrial wastewater. It is necessary to find an effective method to separate and remove soluble ions, organic matter, bacteria, colloidal particles, particles and other pollutants in wastewater, so that wastewater can be reused. Requirements.
  • the present invention provides an advanced wastewater treatment device based on ozone and biofilm granular sludge reactors.
  • the present invention enhances the degradation and removal effect of refractory organic pollutants in wastewater, and significantly The treatment cost is reduced, and the efficiency of advanced wastewater treatment is effectively improved.
  • the present invention provides a wastewater advanced treatment device based on ozone and biofilm granular sludge reactor, which includes: a collection tank, an ozone reactor, a balance adjustment tank, a first water pump, a second water pump, a third water pump and a sequencing batch biological system Membrane granular sludge expanded bed reactor;
  • the water outlet of the sump is connected to the water inlet of the ozone reactor through the first water pump, and the water outlet of the ozone reactor is connected to the water inlet of the equalizing adjustment tank through the second water pump, and the water outlet of the equalizing adjustment tank passes through
  • the third water pump is connected with the water inlet of the expanded bed reactor of the sequencing batch type biofilm granular sludge.
  • the sequencing batch biofilm granular sludge expanded bed reactor is provided with: water inlet, support plate, biological carrier bed, limit plate, water distribution system, air distribution system, water distribution device, aerator Air system, first blower, second blower, circulating water inlet pump and circulating water outlet;
  • the water inlet is connected with the water outlet of the third water pump, the biological carrier bed is arranged on a supporting plate, the biological carrier bed is arranged with biological carriers, the interval between the biological carrier bed and the limiting plate forms an expansion space, and the cloth
  • the air system is connected to the first blower, the water distributor is installed on the support plate, the aeration system is connected to the second blower, the circulating water outlet is connected to the water inlet of the circulating water inlet pump, and the water distributing system is connected to Connect the outlet of the circulating water pump.
  • the volume of the expansion space is set to 1/50-1/20 of the volume of the biological carrier bed.
  • the inner circle of the biological carrier is provided with granular sludge
  • the outer circle is provided with a biofilm
  • the inner circle is provided with partition bars.
  • the biological carrier adopts a hollow particle filler with a density of less than 1 g/cm 3 , a specific surface area greater than 500 m 2 /m 3 and a porosity between 60% and 85%.
  • the support plate adopts a perforated plate, and water distributors are evenly distributed on the through holes of the support plate, and the waste water is evenly distributed along the vertical cross section of the water flow after passing through the water distributor and reacts through the biofilm particle sludge.
  • the biofilm granular sludge reaction zone is equipped with a biological carrier
  • the limiting plate adopts a porous plate
  • the waste water enters the circulation return zone from the biofilm granular sludge reaction zone through the through holes on the limiting plate
  • the limiting plate The size of the through hole is smaller than the size of the biological carrier.
  • the sequencing batch type biofilm granular sludge expanded bed reactor is also provided with a circulating aeration tank and a water outlet tank, and the water outlet tank is provided with a circulating return port, the circulating return port and the circulating aeration tank.
  • Tank connection, the aeration system is arranged in the circulating aeration tank, and the circulating water outlet is arranged on the circulating aeration tank.
  • a wastewater reuse treatment device including: a first pool, a second pool, a third pool, a fourth water pump, a fifth water pump, a sixth water pump, a multi-media filter, and an ultrafiltration membrane system And reverse osmosis system;
  • the sequencing batch type biofilm granular sludge expanded bed reactor is provided with a drain port connected with the water inlet of the first pool, and the water outlet of the first pool is connected to the multi-media filter through a fourth water pump
  • the water inlet is connected, the water outlet of the multi-media filter is connected with the water inlet of the second pool, and the water outlet of the second pool is connected with the water inlet of the ultrafiltration membrane system through the fifth water pump, the ultrafiltration membrane system
  • the water outlet is connected with the water inlet of the third pool, and the water outlet of the third pool is connected with the reverse osmosis system through the sixth water pump.
  • the third pool is provided with a stirring device, a scale inhibitor and an antioxidant input port, and the ultrafiltration membrane treatment system and the reverse osmosis membrane treatment system are both provided with a cleaning liquid inlet.
  • the water collection tank is provided with a catalyst input port
  • the balance adjustment tank is provided with a nutrient salt and lye input port
  • the water collection tank and the balance adjustment tank are both equipped with a stirring device
  • the ozone reactor A gas disperser and an ozone destroyer are arranged, the gas disperser is arranged at the bottom of the ozone reactor and connected with the gas inlet, and the ozone destroyer is arranged at the tail gas outlet of the ozone reactor.
  • the present invention has the following advantages and beneficial effects:
  • the present invention utilizes the synergistic effect of ozone catalytic oxidation and biological treatment of biofilm granular sludge reactor to greatly enhance the degradation and removal effect of refractory organic pollutants in wastewater, significantly reduce treatment costs, and effectively improve wastewater depth Processing efficiency.
  • the sequencing batch biofilm granular sludge expanded bed reactor of the present invention has a high sludge concentration, and the biofilm granular sludge reactor biological carrier bed sludge concentration (TSS) reaches 20-45g/L, which is higher than the current commonly used
  • TSS biological carrier bed sludge concentration
  • the biological carrier of the present invention is provided with granular sludge in the inner circle, biofilm in the outer circle, and partition bars in the inner circle.
  • the formation of granular sludge is the main reason for the high sludge concentration in the reactor.
  • the medium to high concentration granular sludge and biofilm ensure a good wastewater treatment effect.
  • the biological treatment aeration system is set in a separate circulating aeration tank, which solves the problem that the biological treatment system is easy to block the aeration system, and the maintenance of the aeration system is convenient.
  • the circulating aeration system The pond has the function of diluting and equalizing water quality, which is beneficial to improve the efficiency of wastewater treatment.
  • the sequencing batch type biofilm granular sludge expanded bed reactor of the present invention is simple and compact, highly efficient and flexible, and has strong adaptability.
  • the sequencing batch type biofilm granular sludge expanded bed reactor of the present invention is equipped with an expansion space, so that the biological carrier in the biological carrier bed is in a micro-expansion state during the wastewater treatment process, which is beneficial to the wastewater in the biofilm granular sludge.
  • the uniform distribution of the reaction zone and uniform treatment can effectively improve the efficiency of wastewater treatment.
  • Fig. 1 is a schematic structural diagram of a wastewater advanced treatment device based on ozone and biofilm granular sludge reactor of Example 1;
  • Figure 2 is a partial enlarged view of the biological carrier bed at I in Figure 1;
  • Example 3 is a schematic diagram of the structure of the biological carrier of Example 1;
  • Example 5 is a schematic diagram of the structure of the biofilm granular sludge reactor of Example 3.
  • 1-biofilm granular sludge reactor 2-circulating aeration tank, 3-backwashing drainage outlet, 4-first blower, 5-air distribution system, 6-water distribution system, 7-support plate, 8 -Water distributor, 9-biological carrier bed, 10-outlet, 11-expansion space, 12-limiting plate, 13-outlet tank, 14-circulation return port, 15-circulation water inlet pump, 16-water inlet, 17 -Second blower, 18-aeration system, 19-pipe, 20-circulation outlet, 21-sump, 22-first water pump, 23-ozone reactor, 24-gas disperser, 25-ozone destroyer, 26-Second water pump, 27-Balance adjustment tank, 28-Third water pump, 29-Granular sludge, 30-Biofilm, 31-First pool, 32-Fourth water pump, 33-Multi-media filter, 34- The second pool, 35-the fifth water pump, 36-ultrafiltration membrane system, 37-the third pool, 38-the sixth water
  • this embodiment provides a wastewater advanced treatment device based on ozone and biofilm particle sludge reactor, including: a collecting tank 21, an ozone reactor 23, a balance adjustment tank 27 and a batch type biofilm particle Sludge expanded bed reactor.
  • Sequencing batch type biofilm granular sludge expanded bed reactor includes biofilm granular sludge reactor 1 and circulating aeration tank 2;
  • the water outlet of the sump 21 is connected to the water inlet of the ozone reactor 23 through the first water pump 22, and the water outlet of the ozone reactor 23 is connected to the water inlet of the balance adjustment tank 27 through the second water pump 26.
  • the reactor 23 is provided with a gas disperser 24, and an ozone destroyer 25 is provided on the tail gas pipeline;
  • the sump and the balance adjustment tank are both equipped with stirring devices, and the water outlet of the balance adjustment tank 27 is connected to the water inlet 16 of the circulating aeration tank 2 through the third water pump 28;
  • the biofilm granular sludge reactor 1 is provided with a water and gas distribution zone A, a biofilm granular sludge reaction zone B, and a circulation return zone C along the flow direction of the wastewater;
  • Water system 6, air distribution system 5, water distributor 8 installed on support plate 7, said air distribution system 5 is connected to first blower 4 through pipes;
  • said biofilm particle sludge reaction zone B includes support plate 7 , The biological carrier bed 9, the limiting plate 12, and the expansion space 11 between the biological carrier bed 9 and the limiting plate 12 arranged on the supporting plate 7;
  • the circulating return zone C is provided with a water outlet trough 13 and a water outlet trough 13 A circulating return port 14 is provided, and the circulating return port 14 is connected to the circulating aeration tank 2 through a pipe 19;
  • the support plate 7 adopts a perforated plate, and the through hole of the support plate 7 is provided with a water distributor 8 so that the waste water is evenly distributed along the vertical cross section of the water flow and passes through the biofilm particle sludge reaction zone;
  • the limit plate 12 adopts Perforated plate, wastewater enters the circulation return zone from the biofilm particle sludge reaction zone through the through holes on the limiting plate 12, and the size of the through holes on the limiting plate 12 is smaller than the size of the biological carrier in the biofilm particle sludge reaction zone;
  • the circulating aeration tank 2 is provided with an aeration system 18 and a circulating water outlet 20.
  • the aeration system 18 is connected to the second blower 17 through a pipe.
  • the circulating water outlet 20 is connected to the water inlet of the circulating water pump 15 through the pipe. Connection, the water outlet of the circulating water inlet pump 15 is connected to the water distribution system 6;
  • the biofilm granular sludge reactor 1 is also provided with a backwash drain 3;
  • the circulating aeration tank 2 is also provided with a water inlet 16 and a drain 10, and the circulating aeration tank 2 is provided with a water inlet 16 is connected to the outlet of the third water pump 28 through a pipeline;
  • the minimum volume of the expansion space 11 is 0, and the maximum volume of the expansion space 11 is 1/10 of the volume of the biological carrier bed 9; the volume of the expansion space 11 in this embodiment is preferably set to 1 of the volume of the biological carrier bed 9 /50-1/20;
  • the wastewater maintains a certain flow rate when passing through the biological carrier bed 9, so that the biological carrier in the biological carrier bed 9 is in a micro-expanded state.
  • the expansion of the biological carrier can fill the entire space including the biological carrier bed 9 and the expansion space 11.
  • the flow rate is 1.5-15mm/s
  • the biological carrier adopts hollow particle fillers with a density of less than 1 g/cm3, a specific surface area greater than 500m 2 /m 3 and a porosity between 60% and 85%.
  • the biological carrier is in a micro-expansion state during the wastewater treatment process and is irregularly distributed in the biofilm granular sludge reaction zone B; as shown in Figure 3, the biological carrier is surrounded by granular sludge 29.
  • a biofilm 30 is formed in the outer ring, and partitions are arranged in the inner ring.
  • the granular sludge and biofilm are formed at the same time in the reactor.
  • biofilm is formed on the surface of the carrier.
  • the formation of granular sludge is the main reason for the high concentration of sludge in the reactor.
  • the high concentration of granular sludge and biofilm in the reactor Ensure good wastewater treatment effect.
  • the advanced wastewater treatment method of the wastewater advanced treatment device based on ozone and biofilm granular sludge reactor is:
  • the dosage of hydrogen peroxide is 0.20mmol/L
  • the wastewater is treated by secondary biological treatment of paper-making wastewater
  • the COD of wastewater is 147mg/L
  • the color is 67C.U.
  • the SS is 41mg/ L
  • the dosing amount of ozone is 120mg/L, after 20 minutes of catalytic ozone oxidation treatment, stop supplying ozone/oxygen mixed gas to the ozone reactor 23;
  • the wastewater that has undergone ozone pre-oxidation treatment enters the balance adjustment tank 27 through the second water pump 26, and at the same time, adds nutrients and lye required for biological treatment to the balance adjustment tank 27, and mixes them evenly through a stirring device;
  • the waste water in the balance adjustment tank 27 enters the circulating aeration tank 2 from the water inlet 16 through the third water pump 28, and at the same time, the circulating water inlet pump 15 is started, and the waste water in the circulating aeration tank 2 is transported to the circulating water inlet through the circulating water outlet 20 through the circulating water inlet pump 15
  • the water distribution system 6 enters the biofilm granular sludge reactor 1. When the biofilm granular sludge reactor 1 is full of wastewater and the wastewater in the circulating aeration tank 2 reaches a certain level, the water will stop;
  • the wastewater in the circulating aeration tank 2 is transported to the water distribution system 6 of the water distribution area A of the biofilm granular sludge reactor 1 through the circulation water outlet 20 through the circulation water inlet pump 15 and enters the water distribution area A,
  • the wastewater in the water distribution zone A passes through the water distributor 8 on the support plate 7 and enters the biological carrier bed 9 of the biofilm granular sludge reaction zone B; the wastewater undergoes biochemical oxidation treatment in the biological carrier bed 9, and then passes through the limit plate 12 Enter the recirculation zone C;
  • the waste water in the circulating return zone C passes through the circulating return port 14 provided in the water outlet tank 13 and then enters the circulating aeration tank 2 through the pipe 19.
  • the waste water in the circulating aeration tank 2 again passes through the circulating water inlet pump 15 through the biofilm granular sludge.
  • the water and gas distribution zone A, the biofilm granular sludge reaction zone B and the circulation return zone C of the reactor 1 are used for wastewater treatment and circulation;
  • the volume of the expansion space 11 of the biofilm granular sludge reactor 1 is set to 1/20 of the volume of the biological carrier bed 9, the flow rate of the wastewater in the biological carrier bed is 15mm/s, and the wastewater treatment cycle is 6h ,
  • the aeration operation time is 4h
  • the hypoxia operation time is 1h
  • the dissolved oxygen concentration in the biofilm granular sludge reaction zone B during aeration operation is 4-5mg/L;
  • the second blower 17 is stopped to supply air to the circulating aeration tank 2 for a period of time, so that the wastewater is treated and circulated under anoxic conditions;
  • the biological carrier can be backwashed by the first blower 4 and the air distribution system 5, and the backwashed wastewater can be discharged from the reactor through the backwash drain 3.
  • different wastewater treatment effects can be obtained by changing parameters such as the characteristics of the wastewater, the volume of the expansion space 11, the flow rate of the wastewater in the biological carrier bed, the aeration operation time and the anoxic operation time, as described below:
  • the COD of the wastewater to be treated is 165mg/L, the chromaticity is 90C.U., and the SS is 31mg/L.
  • the amount of hydrogen peroxide added is 0.2mmol/L, and the amount of ozone added is 120mg/L.
  • the time is 20min; the volume of the expansion space 11 of the biofilm granular sludge reactor 1 is 1/40 of the volume of the biological carrier bed 9, the flow rate of the wastewater in the biological carrier bed is 8mm/s, and the wastewater treatment cycle is 6h.
  • the aeration operation time is 4h
  • the hypoxia operation time is 1h
  • the dissolved oxygen concentration of the biofilm granular sludge reaction zone B during aeration operation is 4-5mg/L
  • the treated wastewater COD, SS and color are 52mg/L respectively , 14mg/L and 18C.U.;
  • the COD of the wastewater to be treated is 165mg/L, the chromaticity is 90C.U., and the SS is 31mg/L.
  • the amount of hydrogen peroxide added is 0.2mmol/L, and the amount of ozone added is 120mg/L.
  • the time is 20min; the volume of the expansion space 11 of the biofilm granular sludge reactor 1 is 1/50 of the volume of the biological carrier bed 9, the flow rate of the wastewater in the biological carrier bed is 1.5mm/s, and the wastewater treatment cycle is 6h.
  • the aeration operation time is 4.5h
  • the hypoxia operation time is 0.5h
  • the dissolved oxygen concentration in the biofilm particle sludge reaction zone B is 4-5mg/L during aeration operation
  • the COD, SS and chromaticity of the wastewater after treatment are respectively 42mg/L, 10mg/L and 12C.U.
  • the wastewater is first pre-oxidized by ozone/catalytic ozone to significantly improve the biodegradability of the refractory pollutants in the secondary biological treatment effluent, and then the wastewater is subjected to biological treatment, and the pollutants in the wastewater are further degraded and removed by biochemical oxidation.
  • a sequencing batch biofilm granular sludge expanded bed reactor with the advantages of high sludge concentration and low sludge yield is adopted, which greatly improves the efficiency of wastewater biological treatment and reduces treatment costs.
  • This embodiment provides an advanced wastewater treatment device based on ozone and a biofilm granular sludge reactor.
  • the discharge port of the sequencing batch biofilm granular sludge expanded bed reactor is also connected with a wastewater reuse treatment device.
  • the treatment with the treatment device can further remove the non-process ions and other pollutants in the wastewater, so that the wastewater can meet the requirements of reuse;
  • the wastewater reuse treatment device includes: a first pool, a multi-media filter, a second pool, an ultrafiltration membrane system, a third pool, and a reverse osmosis system.
  • the third pool 37 is set There is a stirring device, and the ultrafiltration membrane treatment system 36 and the reverse osmosis membrane treatment system 39 are both equipped with a cleaning system, which uses acids, alkalis, and fungicides for regular cleaning.
  • the water outlet 10 provided in the circulating aeration tank 2 is connected to the first pool 31 through a pipe
  • the multi-media filter 33 is provided with a water inlet and a water outlet; the water inlet provided by the multi-media filter 33 is connected to The water outlet of the fourth water pump 32 is connected, the water inlet of the fourth water pump 32 is connected to the first pool 31 through a pipe, and the water outlet provided by the multi-media filter 33 is connected to the second pool 34 through a pipe;
  • the second pool 34 is connected to the water inlet of the fifth water pump 35 through a pipe, and the water outlet of the fifth water pump 35 is connected to the water inlet of the ultrafiltration membrane system 36 through a pipe.
  • the filtrate outlet of 36 is connected to the third pool 37 through a pipe;
  • the third pool 37 is connected to the water inlet of the sixth water pump 38 through a pipe, and the water outlet of the sixth water pump 38 is connected to the water inlet of the reverse osmosis membrane system 39 through a pipe.
  • the filtrate of 39 is sent back to the water tank and used in the production process;
  • Reverse osmosis membrane treatment After the wastewater in the third pool 37 is evenly mixed with the added scale inhibitors and antioxidants, it is transported to the reverse osmosis membrane system 39 through the sixth water pump 38, and the filter treated by the reverse osmosis membrane system 39 The permeate is sent back to the water tank and reused in the production process.
  • the concentrated liquid of the reverse osmosis membrane treatment system 39 is sent to the reverse osmosis concentrated liquid treatment system. After treatment, it reaches the discharge standard. After the reverse osmosis membrane treatment, the filtrate COD, SS and The chromaticity is 12mg/L, 3mg/L and 0C.U. respectively.
  • the parameters such as the amount of hydrogen peroxide added, the amount of ozone added, the volume of the expansion space of the biofilm granular sludge reactor, the flow rate of the wastewater in the biological carrier bed, the aeration operation time and the anoxic operation time are changed , Can obtain different wastewater treatment effects, as follows:
  • Wastewater COD is 115mg/L, chromaticity is 25C.U., SS is 28mg/L, based on the volume of wastewater, the amount of hydrogen peroxide is 0.35mmol/L, the amount of ozone is 120mg/L, and the treatment time is 20min
  • the volume of the expansion space 11 of the biofilm granular sludge reactor 1 is 1/50 of the volume of the biological carrier bed 9, the flow rate of wastewater in the biological carrier bed is 1.5mm/s, and the wastewater treatment cycle is 6h, in which the aeration operation
  • the time is 4.5h
  • the anoxic operation time is 0.5h
  • the dissolved oxygen concentration in the biofilm granular sludge reaction zone B during aeration operation is 4-5mg/L
  • the COD, SS and chromaticity of the reverse osmosis membrane filtrate after treatment Respectively 7mg/L, 1mg/L and 0C.U.;
  • Wastewater COD is 165mg/L, chromaticity is 90C.U.
  • SS is 31mg/L, based on the volume of wastewater, the addition of hydrogen peroxide is 0.5mmol/L, the addition of ozone is 180mg/L, and the treatment time is 20min ,
  • the volume of the expansion space 11 of the biofilm granular sludge reactor 1 is 1/40 of the volume of the biological carrier bed 9, the flow rate of wastewater in the biological carrier bed is 8mm/s, and the wastewater treatment cycle is 6h, and the aeration operation time is 4h, anoxic operation time is 1h, the dissolved oxygen concentration of biofilm granular sludge reaction zone B during aeration operation is 4-5mg/L, after treatment the COD, SS and chromaticity of the reverse osmosis membrane filtrate are 15mg respectively /L, 4mg/L and 0C.U.
  • the wastewater is first pre-oxidized by ozone/catalytic ozone to significantly improve the biodegradability of the refractory pollutants in the effluent from the secondary biological treatment. Then the wastewater is subjected to biological treatment, and the organic matter in the wastewater is further degraded and removed by biochemical oxidation. Pollutants, then, the wastewater is treated by a multi-media filter, ultrafiltration membrane system and reverse osmosis membrane system to further remove non-process ions and other pollutants in the wastewater, so that the wastewater can meet the requirements for reuse.
  • the biofilm granular sludge reactor can also adopt an integrated structure, and the aeration system is separately arranged in the circulation return zone C, which can also achieve the purpose of convenient maintenance.
  • the biofilm granular sludge reactor of this embodiment is sequentially provided with a water and gas distribution zone, a biofilm granular sludge reaction zone and a circulation return zone along the wastewater treatment flow direction;
  • the biofilm granular sludge reaction zone includes a supporting plate 7, a biological carrier bed 9, a limiting plate 12 and an expansion space 11.
  • the biological carrier bed 9 is arranged on the supporting plate 7, and the distance between the biological carrier bed 9 and the limiting plate 12
  • An expansion space 11 is formed;
  • the water distribution area is provided with a water distribution system 6, an air distribution system 5, a water distributor 8 and a first blower 4.
  • the air distribution system 5 is connected to the first blower 4, and the water distributor 8 is installed on the support On the board 7;
  • the circulating return zone is provided with an aeration system 18, a second blower 17, a circulating water inlet pump 15 and a circulating water outlet 20.
  • the circulating water outlet 20 is connected to the water inlet of the circulating water pump 15, and the water distribution system 6 is connected to the circulating inlet
  • the water outlet of the water pump 15 is connected, and the aeration system 18 is connected with the second blower 17.
  • the biofilm granular sludge reactor of this embodiment is also provided with a water inlet 16, a drain 10, and a backwash drain 3.
  • the water inlet 16 is provided in the circulating return zone C, the water inlet 16 and the third water pump 28 Connected, the drainage outlet is located in the biofilm particle sludge reaction zone B, and the backwashing drainage outlet is located in the water and gas distribution zone A.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Biological Treatment Of Waste Water (AREA)

Abstract

一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，包括：集水池(21)、臭氧反应器(23)、均衡调节池(27)、第一水泵(22)、第二水泵(26)、第三水泵(28)、序批式生物膜颗粒污泥膨胀床反应器以及废水回用处理装置；集水池(21)通过第一水泵(22)与臭氧反应器(23)连接，臭氧反应器(23)通过第二水泵(26)与均衡调节池(27)连接，均衡调节池(27)通过第三水泵(28)与序批式生物膜颗粒污泥膨胀床反应器连接；废水回用处理装置包括：第一水池(31)，第二水池(34)、第三水池(37)、第四水泵(32)、第五水泵(35)、第六水泵(38)、多介质过滤器(33)、超滤膜系统(36)和反渗透膜系统(39)；该装置利用臭氧催化氧化和生物膜颗粒污反应器生物处理的协同效应，增强了对废水中难降解有机污染物的降解去除效果，降低了处理成本，提高了废水深度处理的效率。

Description

基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置 技术领域
本发明涉及废水深度处理技术领域，具体涉及一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置。
背景技术
随着环境保护标准的不断提高，在现代工业废水处理工艺流程中，很多工业废水经二级生物处理后不能达到排放标准，必须进行进一步的深度处理，例如，造纸废水中因含有一定浓度的木素降解产物，经二级生物处理后仍然含有较高浓度的有机污染物，不能达到国家的排放标准，必须进行进一步的处理，以减轻对环境的影响。
Fenton氧化技术是当前降解去除废水中难降解有机物的有效途径之一，首先在酸性条件下亚铁离子催化过氧化氢分解产生羟基自由基，通过羟基自由基氧化降解、矿化废水中的有机污染物；然后调节反应体系的pH值至中、碱性，铁离子生成铁盐沉淀絮体，通过吸附、混凝、沉淀的方式去除废水中的有机污染物、悬浮物和其他污染物。但是Fenton氧化技术存在着化学品用量大、处理成本高的问题，且处理过程中产生了大量的含铁化学污泥，成为Fenton氧化技术进一步推广应用的障碍。另一方面，非过程离子是工业废水循环回用的另一个障碍，需要寻找一种分离去除废水中可溶性离子、有机物、细菌、胶体粒子、微粒及其他污染物的有效方法，使废水达到回用水的要求。
发明内容
为了克服现有技术存在的缺陷与不足，本发明提供一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，本发明增强了对废水中难降解有机污染物的降解去除效果，显著降低了处理成本，有效提高了废水深度处理的效率。
为了达到上述目的，本发明采用以下技术方案：
本发明提供一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，包括：集水池、臭氧反应器、均衡调节池、第一水泵、第二水泵、第三水泵和序批式生物膜颗粒污泥膨胀床反应器；
所述集水池的出水口通过第一水泵与臭氧反应器的进水口连接，所述臭氧反应器的出水口通过第二水泵与均衡调节池的进水口连接，所述均衡调节池的出水口通过第三水泵与序批式生物膜颗粒污泥膨胀床反应器进水口连接。
作为优选的技术方案，所述序批式生物膜颗粒污泥膨胀床反应器设有：进水口、支撑板、生物载体床、限位板、布水系统、布气系统、布水器、曝气系统、第一鼓风机、第二鼓风机、循环进水泵和循环出水口；
所述进水口与第三水泵的出水口连接，所述生物载体床设置在支撑板上，所述生物载体床设置有生物载体，生物载体床与限位板的间隔形成膨胀空间，所述布气系统与第一鼓风机连接，所述布水器安装在支撑板上，所述曝气系统与第二鼓风机连接，所述循环出水口与循环进水泵的进水口连接，所述布水系统与循环进水泵的出水口连接。
作为优选的技术方案，所述膨胀空间的容积设置为生物载体床容积的1/50-1/20。
作为优选的技术方案，所述生物载体内圈设有颗粒污泥，外圈设有生物膜，内圈内设有分隔条。
作为优选的技术方案，所述生物载体采用密度小于1g/cm 3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
作为优选的技术方案，所述支撑板采用多孔板，所述支撑板的通孔上均匀分布设置布水器，废水经布水器后沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区，所述生物膜颗粒污泥反应区设有生物载体，所述限位板采用多孔板，废水经限位板上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位 板上的通孔尺寸小于所述生物载体的尺寸。
作为优选的技术方案，所述序批式生物膜颗粒污泥膨胀床反应器还设有循环曝气池和出水槽，所述出水槽设置有循环回流口，所述循环回流口与循环曝气池连接，所述曝气系统设置在循环曝气池内，所述循环出水口设置在循环曝气池上。
作为优选的技术方案，还设置有废水回用处理装置，包括：第一水池、第二水池、第三水池、第四水泵、第五水泵、第六水泵、多介质过滤器、超滤膜系统和反渗透系统；
所述序批式生物膜颗粒污泥膨胀床反应器设置有排水口，所述排水口与第一水池的进水口连接，所述第一水池的出水口通过第四水泵与多介质过滤器的进水口连接，所述多介质过滤器的出水口与第二水池的进水口连接，所述第二水池的出水口通过第五水泵与超滤膜系统的进水口连接，所述超滤膜系统的出水口与第三水池的进水口连接，所述第三水池的出水口通过第六水泵与反渗透系统连接。
作为优选的技术方案，所述第三水池设置有搅拌装置、阻垢剂和抗氧化剂投入口，所述超滤膜处理系统和反渗透膜处理系统均设置有清洗液入口。
作为优选的技术方案，所述集水池设有催化剂投入口，所述均衡调节池设有营养盐和碱液投入口，所述集水池和均衡调节池均设置有搅拌装置，所述臭氧反应器设置有气体分散器和臭氧破坏器，所述气体分散器设置在臭氧反应器底部并与气体入口连接，所述臭氧破坏器设置在臭氧反应器尾气出口。
本发明与现有技术相比，具有如下优点和有益效果：
(1)本发明利用臭氧催化氧化和生物膜颗粒污泥反应器生物处理的协同效应，大大增强了对废水中难降解有机污染物的降解去除效果，显著降低了处理 成本，有效提高了废水深度处理的效率。
(2)本发明的序批式生物膜颗粒污泥膨胀床反应器污泥浓度高，生物膜颗粒污泥反应器生物载体床污泥浓度(TSS)达到20-45g/L，高于目前常用的活性污泥法和生物膜法的污泥浓度，保证废水处理获得良好的效果。
(3)本发明的生物载体内圈设有颗粒污泥，外圈设有生物膜，内圈内设有分隔条，颗粒污泥的形成是反应器具有高污泥浓度的主要原因，反应器中高浓度的颗粒污泥和生物膜保证了良好的废水处理效果。
(4)本发明将生物处理的曝气系统设置在单独的循环曝气池中，解决了生物处理系统普遍存在的曝气系统容易堵塞的问题，且曝气系统维护方便，同时，循环曝气池具有稀释、均衡水质的作用，有利于提高废水处理效率。
(5)本发明的序批式生物膜颗粒污泥膨胀床反应器简洁紧凑、高效灵活、适应性强。
(6)本发明的序批式生物膜颗粒污泥膨胀床反应器设置了膨胀空间，使废水处理过程中生物载体床中的生物载体处于微膨胀化状态，有利于废水在生物膜颗粒污泥反应区的均匀分布，受到均匀的处理，有效提高了废水处理的效率。
附图说明
图1为本实施例1的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置结构示意图；
图2为图1中I处生物载体床的局部放大图；
图3为本实施例1的生物载体结构示意图；
图4为本实施例2的废水回用处理装置结构示意图；
图5为本实施例3的生物膜颗粒污泥反应器的结构示意图。
其中，1-生物膜颗粒污泥反应器，2-循环曝气池，3-反冲洗排水口，4-第一鼓风机，5-布气系统，6-布水系统，7-支撑板，8-布水器，9-生物载体床，10-排水口，11-膨胀空间，12-限位板，13-出水槽，14-循环回流口，15-循环进水泵，16-进水口，17-第二鼓风机，18-曝气系统，19-管道，20-循环出水口，21-集水池，22-第一水泵，23-臭氧反应器，24-气体分散器，25-臭氧破坏器，26-第二水泵，27-均衡调节池，28-第三水泵，29-颗粒污泥，30-生物膜，31-第一水池，32-第四水泵，33-多介质过滤器，34-第二水池，35-第五水泵，36-超滤膜系统，37-第三水池，38-第六水泵，39-反渗透膜系统。
具体实施方式
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图及实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅仅用以解释本发明，并不用于限定本发明。
实施例1
如图1所示，本实施例提供一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，包括：集水池21、臭氧反应器23、均衡调节池27和序批式生物膜颗粒污泥膨胀床反应器，序批式生物膜颗粒污泥膨胀床反应器包括生物膜颗粒污泥反应器1和循环曝气池2；
在本实施例中，集水池21的出水口通过第一水泵22与臭氧反应器23的进水口连接，臭氧反应器23的出水口通过第二水泵26与均衡调节池27的进水口连接，臭氧反应器23设置有气体分散器24，在尾气管道上设有臭氧破坏器25；
在本实施例中，集水池和均衡调节池均设置有搅拌装置，均衡调节池27的出水口通过第三水泵28与循环曝气池2的进水口16连接；
在本实施例中，生物膜颗粒污泥反应器1沿废水流动方向设置有布水布气区A、生物膜颗粒污泥反应区B和循环回流区C；布水布气区A设有布水系统6、布气系统5、安装在支撑板7上的布水器8，所述布气系统5通过管道和第一鼓风机4连接；所述生物膜颗粒污泥反应区B包括支撑板7、设置在支撑板7上面的生物载体床9、限位板12、位于生物载体床9与限位板12之间的膨胀空间11；所述循环回流区C设置有出水槽13，出水槽13设置有循环回流口14，循环回流口14通过管道19与循环曝气池2连接；
在本实施例中，支撑板7采用多孔板，支撑板7的通孔上设置布水器8，使废水沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区；限位板12采用多孔板，废水经限位板12上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位板12上的通孔尺寸小于生物膜颗粒污泥反应区中的生物载体的尺寸；
在本实施例中，循环曝气池2设置有曝气系统18和循环出水口20，曝气系统18通过管道和第二鼓风机17连接，循环出水口20通过管道与循环进水泵15的进水口连接，循环进水泵15的出水口与布水系统6连接；
在本实施例中，生物膜颗粒污泥反应器1上还设置有反冲洗排水口3；循环曝气池2上还设置有进水口16和排水口10，循环曝气池2设置的进水口16通过管道与第三水泵28的出水口连接；
在本实施例中，膨胀空间11的最小容积为0，膨胀空间11的最大容积是生物载体床9容积的1/10；本实施例膨胀空间11的容积优选设置为生物载体床9容积的1/50-1/20；
在本实施例中，废水通过生物载体床9时维持一定的流速，使生物载体床9中的生物载体处于微膨胀化状态，生物载体膨胀可以充满包括生物载体床9和膨胀空间11的整个空间，优选流速为1.5-15mm/s，生物载体采用密度小于1 g/cm3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
如图2所示，生物载体在废水处理过程中处于微膨胀化状态，无规律分布在生物膜颗粒污泥反应区B内；如图3所示，生物载体内圈设有颗粒污泥29，外圈形成生物膜30，内圈内设有分隔条，反应器同时形成了颗粒污泥和生物膜，颗粒污泥和生物膜同时存在好氧、兼氧和厌氧微生物群落；当反应器污泥驯化完成后，生物载体中产生了颗粒污泥，而载体表面形成了生物膜，颗粒污泥的形成是反应器具有高污泥浓度的主要原因，反应器中高浓度的颗粒污泥和生物膜保证了良好的废水处理效果。
本实施例基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置的废水深度处理方法为：
S1：臭氧预氧化处理：
向集水池21中加入过氧化氢作为臭氧催化剂，并启动集水池21的搅拌装置搅拌均匀，接着集水池21中的二级生物处理出水(投加催化剂的废水)通过第一水泵22进入臭氧反应器23，到达一定液位后停止进水；接着，来自臭氧发生系统的臭氧/氧气混合气体通过气体分散器24分散进入臭氧反应器23，对臭氧反应器23中的废水进行臭氧预氧化处理，臭氧氧化处理20min后，停止向臭氧反应器23供应臭氧/氧气混合气体；
在本实施例中，过氧化氢的投加量为0.20mmol/L，废水采用造纸涂布废水二级生物处理出水，废水COD为147mg/L，色度为67C.U.，SS为41mg/L，臭氧投加量为120mg/L，催化臭氧氧化处理20min后，停止向臭氧反应器23供应臭氧/氧气混合气体；
S2：废水的均衡调节：
经过臭氧预氧化处理的废水通过第二水泵26进入均衡调节池27，同时向均 衡调节池27加入生物处理所需补充的营养盐和碱液，并通过搅拌装置混合均匀；
S3：均衡调节池27的废水进行生物化学氧化处理：
1)进水
均衡调节池27中的废水通过第三水泵28从进水口16进入循环曝气池2，同时启动循环进水泵15，循环曝气池2中的废水通过循环出水口20经循环进水泵15输送到布水系统6，进入生物膜颗粒污泥反应器1，当生物膜颗粒污泥反应器1充满废水且循环曝气池2中废水到达一定水位后停止进水；
2)废水的处理和循环
进水完成后，启动第二鼓风机17通过曝气系统18对循环曝气池2中的废水进行曝气；
循环曝气池2中的废水通过循环出水口20经循环进水泵15输送到生物膜颗粒污泥反应器1的布水布气区A的布水系统6，进入布水布气区A，布水布气区A的废水通过支撑板7上的布水器8，进入生物膜颗粒污泥反应区B的生物载体床9；废水在生物载体床9进行生物化学氧化处理，然后通过限位板12进入循环回流区C；
循环回流区C中的废水通过设置在出水槽13的循环回流口14后经管道19进入循环曝气池2，循环曝气池2中的废水再次经循环进水泵15依次通过生物膜颗粒污泥反应器1的布水布气区A、生物膜颗粒污泥反应区B和循环回流区C，进行废水的处理和循环；
在本实施例中，生物膜颗粒污泥反应器1的膨胀空间11的容积设置为生物载体床9容积的1/20，废水在生物载体床的流速为15mm/s，废水一个处理周期为6h，其中曝气运行时间为4h，缺氧运行时间为1h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L；
在本实施例中，废水的处理和循环过程中，停止第二鼓风机17向循环曝气池2供气一段时间，使废水在缺氧状态下处理和循环；
3)排水
废水在处理一定时间后，停止循环进水泵15和第二鼓风机17运行，通过排水口10将生物膜颗粒污泥反应器1和循环曝气池2中占废水总量的30％的水排出反应器，经处理后废水COD、SS和色度分别为67mg/L、12mg/L和15C.U.。
在本实施例中，处理废水一段时间后，可以通过第一鼓风机4和布气系统5对生物载体进行反冲洗，通过反冲洗排水口3将反冲洗后的废水排出反应器。
在本实施例中，通过改变废水特性、膨胀空间11的容积、废水在生物载体床的流速、曝气运行时间和缺氧运行时间等参数，可以得到不同的废水处理效果，具体如下所述：
需处理废水的COD为165mg/L，色度为90C.U.，SS为31mg/L，以废水体积计，过氧化氢加入量为0.2mmol/L，臭氧投加量为120mg/L，处理时间为20min；生物膜颗粒污泥反应器1的膨胀空间11的容积为生物载体床9容积的1/40，废水在生物载体床的流速为8mm/s，废水一个处理周期为6h，其中曝气运行时间为4h，缺氧运行时间为1h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后废水COD、SS和色度分别为52mg/L、14mg/L和18C.U.；
需处理废水的COD为165mg/L，色度为90C.U.，SS为31mg/L，以废水体积计，过氧化氢加入量为0.2mmol/L，臭氧投加量为120mg/L，处理时间为20min；生物膜颗粒污泥反应器1的膨胀空间11的容积为生物载体床9容积的1/50，废水在生物载体床的流速为1.5mm/s，废水一个处理周期为6h，其中曝气运行时间为4.5h，缺氧运行时间为0.5h，曝气运行时生物膜颗粒污泥反应区 B溶解氧浓度为4-5mg/L，经处理后废水COD、SS和色度分别为42mg/L、10mg/L和12C.U.。
本实施例中废水首先通过臭氧/催化臭氧预氧化，显著改善二级生物处理出水中难降解污染物的生物降解性，然后废水进行生物处理，通过生物化学氧化进一步降解去除废水中的污染物，本实施例采用具有污泥浓度高、污泥产率低等优点的序批式生物膜颗粒污泥膨胀床反应器，大大提高了废水生物处理的效率，同时减少了处理成本。
实施例2
本实施例2的技术方案除了下述技术特征外，其它技术方案与实施例1相同：
本实施例提供一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，在序批式生物膜颗粒污泥膨胀床反应器的排水口还连接有废水回用处理装置，经过废水回用处理装置的处理，能进一步去除废水中的非过程离子和其他污染物，使废水达到回用水的要求；
如图4所示，在本实施例中，废水回用处理装置包括：第一水池，多介质过滤器、第二水池、超滤膜系统、第三水池和反渗透系统，第三水池37设置有搅拌装置，超滤膜处理系统36和反渗透膜处理系统39均设置有清洗系统，采用酸、碱、杀菌剂等进行定期清洗。
在本实施例中，循环曝气池2设置的排水口10通过管道与第一水池31连接，多介质过滤器33设置有进水口和排水口；多介质过滤器33设置的进水口通过管道与第四水泵32的出水口连接，第四水泵32的进水口通过管道与第一水池31连接，多介质过滤器33设置的排水口通过管道与第二水池34连接；
在本实施例中，第二水池34通过管道与第五水泵35的进水口连接，所述第五水泵35的出水口通过管道与超滤膜系统36的进水口连接，所述超滤膜系统36的滤过液出水口通过管道与第三水池37连接；
在本实施例中，第三水池37通过管道与第六水泵38的进水口连接，所述第六水泵38的出水口通过管道与反渗透膜系统39的进水口连接，所述反渗透膜系统39的滤过液送回用水池，回用于生产过程；
本实施例基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置的废水处理方法为：
S1：臭氧预氧化处理；
S2：废水的均衡调节：经臭氧预氧化处理的废水进入均衡调节池27，同时向均衡调节池27加入生物处理所需补充的营养物和碱液，并通过搅拌混合均匀；
S3：均衡调节池27的废水进行生物化学氧化处理；
S4：多介质过滤：第一水池31中的废水通过第四水泵32输送进入多介质过滤器33，经多介质过滤器33处理后的废水进入第二水池34；
S5：超滤膜处理：第二水池34中的废水通过第五水泵35输送进入超滤膜系统36，经超滤膜系统36处理的滤过液进入第三水池37，超滤膜处理系统36的浓液送回集水池21，和二级生物处理出水混合进行深度处理；
S6：反渗透膜处理：第三水池37中的废水与投加的阻垢剂和抗氧化剂混合均匀后，通过第六水泵38输送进入反渗透膜系统39，经反渗透膜系统39处理的滤过液送回用水池，回用于生产过程，反渗透膜处理系统39的浓液送到反渗透浓液处理系统，经处理后达标排放，经反渗透膜处理后滤过液COD、SS和色度分别为12mg/L、3mg/L和0C.U.。
在本实施例中，通过改变过氧化氢加入量、臭氧投加量、生物膜颗粒污泥 反应器膨胀空间的容积、废水在生物载体床的流速、曝气运行时间和缺氧运行时间等参数，可以得到不同的废水处理效果，具体如下所述：
废水COD为115mg/L，色度为25C.U.，SS为28mg/L，以废水体积计，过氧化氢加入量为0.35mmol/L，臭氧投加量为120mg/L，处理时间为20min，生物膜颗粒污泥反应器1的膨胀空间11的容积为生物载体床9容积的1/50，废水在生物载体床的流速为1.5mm/s，废水一个处理周期为6h，其中曝气运行时间为4.5h，缺氧运行时间为0.5h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后反渗透膜滤过液COD、SS和色度分别为7mg/L、1mg/L和0C.U.；
废水COD为165mg/L，色度为90C.U.，SS为31mg/L，以废水体积计，过氧化氢加入量为0.5mmol/L，臭氧投加量为180mg/L，处理时间为20min，生物膜颗粒污泥反应器1的膨胀空间11的容积为生物载体床9容积的1/40，废水在生物载体床的流速为8mm/s，废水一个处理周期为6h，其中曝气运行时间为4h，缺氧运行时间为1h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后反渗透膜滤过液COD、SS和色度分别为15mg/L、4mg/L和0C.U.。
在本实施例中，废水首先通过臭氧/催化臭氧预氧化，显著改善二级生物处理出水中难降解污染物的生物降解性，然后废水进行生物处理，通过生物化学氧化进一步降解去除废水中的有机污染物，接着，废水经过多介质过滤器、超滤膜系统和反渗透膜系统的处理，进一步去除废水中的非过程离子和其他污染物，使废水达到回用水的要求。
实施例3
本实施例3的技术方案除了下述技术特征外，其它技术方案与实施例1相同：
如图5所示，生物膜颗粒污泥反应器也可以采用一体式结构，并且将曝气系统单独设置在循环回流区C，也能达到方便维护的目的。
本实施例的生物膜颗粒污泥反应器沿废水处理流向上依次设置有布水布气区、生物膜颗粒污泥反应区和循环回流区；
其中，生物膜颗粒污泥反应区包括支撑板7、生物载体床9、限位板12和膨胀空间11，生物载体床9设置在支撑板7上，生物载体床9与限位板12的间隔形成膨胀空间11；布水布气区设置有布水系统6、布气系统5、布水器8和第一鼓风机4，布气系统5与第一鼓风机4连接，布水器8安装在支撑板7上；循环回流区设置有曝气系统18、第二鼓风机17、循环进水泵15和循环出水口20，循环出水口20与循环进水泵15的进水口连接，布水系统6与循环进水泵15的出水口连接，曝气系统18与第二鼓风机17连接。
本实施例的生物膜颗粒污泥反应器上还设置有进水口16、排水口10和反冲洗排水口3，本实施例进水口16设在循环回流区C，进水口16与第三水泵28连接，排水口设在生物膜颗粒污泥反应区B，反冲洗排水口设在布水布气区A。
上述实施例为本发明较佳的实施方式，但本发明的实施方式并不受上述实施例的限制，其他的任何未背离本发明的精神实质与原理下所作的改变、修饰、替代、组合、简化，均应为等效的置换方式，都包含在本发明的保护范围之内。

Claims (10)

  1. 一种基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，包括：集水池、臭氧反应器、均衡调节池、第一水泵、第二水泵、第三水泵和序批式生物膜颗粒污泥膨胀床反应器；
    所述集水池的出水口通过第一水泵与臭氧反应器的进水口连接，所述臭氧反应器的出水口通过第二水泵与均衡调节池的进水口连接，所述均衡调节池的出水口通过第三水泵与序批式生物膜颗粒污泥膨胀床反应器进水口连接。
  2. 根据权利要求1所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述序批式生物膜颗粒污泥膨胀床反应器设有：进水口、支撑板、生物载体床、限位板、布水系统、布气系统、布水器、曝气系统、第一鼓风机、第二鼓风机、循环进水泵和循环出水口；
    所述进水口与第三水泵的出水口连接，所述生物载体床设置在支撑板上，所述生物载体床设置有生物载体，所述生物载体无规律分散布置，所述生物载体床与限位板的间隔形成膨胀空间，所述布气系统与第一鼓风机连接，所述布水器安装在支撑板上，所述曝气系统与第二鼓风机连接，所述循环出水口与循环进水泵的进水口连接，所述布水系统与循环进水泵的出水口连接。
  3. 根据权利要求2所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述膨胀空间的容积设置为生物载体床容积的1/50-1/20。
  4. 根据权利要求2所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述生物载体内圈设有颗粒污泥，外圈设有生物膜，内圈内设有分隔条。
  5. 根据权利要求2或4所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述生物载体采用密度小于1g/cm 3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
  6. 根据权利要求2所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述支撑板采用多孔板，所述支撑板的通孔上均匀分布 设置布水器，废水经布水器后沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区，所述限位板采用多孔板，废水经限位板上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位板上的通孔尺寸小于所述生物载体的尺寸。
  7. 根据权利要求2所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述序批式生物膜颗粒污泥膨胀床反应器还设有循环曝气池和出水槽，所述出水槽设置有循环回流口，所述循环回流口与循环曝气池连接，所述曝气系统设置在循环曝气池内，所述循环出水口设置在循环曝气池上。
  8. 根据权利要求1所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，还设置有废水回用处理装置，包括：第一水池，第二水池、第三水池、第四水泵、第五水泵、第六水泵、多介质过滤器、超滤膜系统和反渗透系统；
    所述序批式生物膜颗粒污泥膨胀床反应器设置有排水口，所述排水口与第一水池的进水口连接，所述第一水池的出水口通过第四水泵与多介质过滤器的进水口连接，所述多介质过滤器的出水口与第二水池的进水口连接，所述第二水池的出水口通过第五水泵与超滤膜系统的进水口连接，所述超滤膜系统的出水口与第三水池的进水口连接，所述第三水池的出水口通过第六水泵与反渗透系统连接。
  9. 根据权利要求8所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述第三水池设置有搅拌装置、阻垢剂和抗氧化剂投入口，所述超滤膜处理系统和反渗透膜处理系统均设置有清洗液入口。
  10. 根据权利要求1所述的基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置，其特征在于，所述集水池设有催化剂投入口，所述均衡调节池设有营养盐和碱液投入口，所述集水池和均衡调节池均设置有搅拌装置，所述臭氧反应器设置有气体分散器和臭氧破坏器，所述气体分散器设置在臭氧反应器底 部并与气体入口连接，所述臭氧破坏器设置在臭氧反应器尾气出口。
PCT/CN2019/124744 2019-07-31 2019-12-12 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置 Ceased WO2021017366A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201910702353.9 2019-07-31
CN201910702353.9A CN110451718B (zh) 2019-07-31 2019-07-31 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置

Publications (1)

Publication Number Publication Date
WO2021017366A1 true WO2021017366A1 (zh) 2021-02-04

Family

ID=68484339

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2019/124744 Ceased WO2021017366A1 (zh) 2019-07-31 2019-12-12 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置

Country Status (2)

Country Link
CN (1) CN110451718B (zh)
WO (1) WO2021017366A1 (zh)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114262117A (zh) * 2021-12-07 2022-04-01 中煤能源研究院有限责任公司 一种有机废水深度降解cod的系统及工艺
CN115925097A (zh) * 2021-08-23 2023-04-07 中国石油化工股份有限公司 一种好氧膨胀床装置及其应用
CN118108366A (zh) * 2024-03-13 2024-05-31 青岛中通臭氧科技有限公司 可持续沿海地下卤水养殖污水回用工艺

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110451718B (zh) * 2019-07-31 2024-07-12 华南理工大学 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置
CN111732182A (zh) * 2020-07-03 2020-10-02 西安建筑科技大学 一种利用催化臭氧氧化消除污泥膨胀的方法及装置
CN114864126A (zh) * 2022-04-01 2022-08-05 中国科学院上海应用物理研究所 一种放射性废液空气载带排放装置

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008007530A1 (de) * 2008-02-05 2009-08-06 Multi Umwelttechnologie Ag Rotationsverfahren und Reaktor zur biologischen Reinigung von Wasser, Prozesswasser und Abwasser
CN101913732A (zh) * 2010-08-04 2010-12-15 中国海洋大学 序批式悬浮填料生物膜污水处理装置
CN102372362A (zh) * 2011-09-30 2012-03-14 东北林业大学 一体化生物膜-颗粒污泥耦合反应器及利用其对污水进行同步脱氮除磷的方法
CN103547535A (zh) * 2011-04-04 2014-01-29 威立雅水务解决方案与技术支持公司 改进的生物污水净化反应器和方法
CN104003590A (zh) * 2014-06-19 2014-08-27 上海环境卫生工程设计院 以低温等离子体耦合生物法处理垃圾渗滤液的装置及方法
CN104150590A (zh) * 2014-07-17 2014-11-19 浙江大学 高效经济的同步去除硝氮和氨氮的生物反应器
CN104193007A (zh) * 2014-09-26 2014-12-10 上海恒致环境科技有限公司 悬浮填料生物膜反应器
CN105693006A (zh) * 2014-11-27 2016-06-22 中国石油天然气股份有限公司 一种好氧生化耦合臭氧催化氧化与生物脱氮处理丙烯腈污水的组合工艺
CN110407410A (zh) * 2019-07-31 2019-11-05 华南理工大学 一种基于生物膜颗粒污泥反应器的废水处理装置及其方法
CN110451718A (zh) * 2019-07-31 2019-11-15 华南理工大学 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104140179B (zh) * 2013-05-07 2016-02-10 中国石化工程建设有限公司 一种废水处理系统及方法
CN203602403U (zh) * 2013-12-12 2014-05-21 无锡通田博适环境科技有限公司 厌氧膨胀床生物膜反应器
CN109851156A (zh) * 2018-12-29 2019-06-07 中冶赛迪工程技术股份有限公司 一种玻纤废水回用处理方法及系统
CN210796108U (zh) * 2019-07-31 2020-06-19 华南理工大学 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008007530A1 (de) * 2008-02-05 2009-08-06 Multi Umwelttechnologie Ag Rotationsverfahren und Reaktor zur biologischen Reinigung von Wasser, Prozesswasser und Abwasser
CN101913732A (zh) * 2010-08-04 2010-12-15 中国海洋大学 序批式悬浮填料生物膜污水处理装置
CN103547535A (zh) * 2011-04-04 2014-01-29 威立雅水务解决方案与技术支持公司 改进的生物污水净化反应器和方法
CN102372362A (zh) * 2011-09-30 2012-03-14 东北林业大学 一体化生物膜-颗粒污泥耦合反应器及利用其对污水进行同步脱氮除磷的方法
CN104003590A (zh) * 2014-06-19 2014-08-27 上海环境卫生工程设计院 以低温等离子体耦合生物法处理垃圾渗滤液的装置及方法
CN104150590A (zh) * 2014-07-17 2014-11-19 浙江大学 高效经济的同步去除硝氮和氨氮的生物反应器
CN104193007A (zh) * 2014-09-26 2014-12-10 上海恒致环境科技有限公司 悬浮填料生物膜反应器
CN105693006A (zh) * 2014-11-27 2016-06-22 中国石油天然气股份有限公司 一种好氧生化耦合臭氧催化氧化与生物脱氮处理丙烯腈污水的组合工艺
CN110407410A (zh) * 2019-07-31 2019-11-05 华南理工大学 一种基于生物膜颗粒污泥反应器的废水处理装置及其方法
CN110451718A (zh) * 2019-07-31 2019-11-15 华南理工大学 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115925097A (zh) * 2021-08-23 2023-04-07 中国石油化工股份有限公司 一种好氧膨胀床装置及其应用
CN114262117A (zh) * 2021-12-07 2022-04-01 中煤能源研究院有限责任公司 一种有机废水深度降解cod的系统及工艺
CN118108366A (zh) * 2024-03-13 2024-05-31 青岛中通臭氧科技有限公司 可持续沿海地下卤水养殖污水回用工艺

Also Published As

Publication number Publication date
CN110451718B (zh) 2024-07-12
CN110451718A (zh) 2019-11-15

Similar Documents

Publication Publication Date Title
WO2021017366A1 (zh) 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置
CN101830595B (zh) 一种制革工业废水的处理方法
CN101525202A (zh) 一种印染废水深度处理与中水回用系统及方法
CN111573991B (zh) 一种化学镀综合废水处理方法
CN101074141B (zh) 低浓度有机废水再生回用工艺
WO2021017367A1 (zh) 一种基于生物膜颗粒污泥反应器的废水处理装置及其方法
CN101318758A (zh) 一种气浮与生物滤池相结合的水处理工艺
CN102372401A (zh) 铁炭微电解-动态膜废水深度处理工艺
CN103755092B (zh) 一种新型纺织染整废水深度处理及回用工艺
CN216808506U (zh) 一种餐厨、厨余垃圾废水的处理系统
CN101544448A (zh) 一种城市污水回用于循环冷却水和电厂锅炉给水的方法
CN106219884A (zh) 高氨氮垃圾渗滤液的处理方法
CN111762965A (zh) 一种石油化工废水深度处理回收利用方法
CN116216990A (zh) 一种垃圾渗滤液电化学处理系统
CN110818205A (zh) 一种降低钢铁综合废水污染物浓度的系统及工艺
CN108545885A (zh) 一种筒纱印染废水分质处理及回用集成化工艺
CN101676230A (zh) 催化铁内电解与悬浮填料生物膜一体化处理工业废水方法
KR101603540B1 (ko) 혐기성화 인터배리어 및 유동상 담체를 구비한 고농도의 질소 제거 및 슬러지 저감형 하수처리 시스템
CN210796108U (zh) 基于臭氧和生物膜颗粒污泥反应器的废水深度处理装置
CN210795919U (zh) 颗粒污泥复合生物膜膨胀床反应器
CN212174735U (zh) 一种用于处理橡胶助剂cbs生产废水的系统
CN106430846A (zh) 一种低有机物含量难生物降解废水高效处理集成工艺
CN112624523B (zh) 一种纺织印染废水的处理方法
CN102807299B (zh) 一种二甲醚生产废水处理与回用的专用装置
CN110436624A (zh) 颗粒污泥复合生物膜膨胀床反应器及其废水处理方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19939686

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 19939686

Country of ref document: EP

Kind code of ref document: A1

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205 DATED 22/03/2022)

122 Ep: pct application non-entry in european phase

Ref document number: 19939686

Country of ref document: EP

Kind code of ref document: A1