CN106986448B - Coupling device of modified rice hull-ultrafiltration membrane bioreactor and method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water - Google Patents

Coupling device of modified rice hull-ultrafiltration membrane bioreactor and method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water Download PDF

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CN106986448B
CN106986448B CN201710265878.1A CN201710265878A CN106986448B CN 106986448 B CN106986448 B CN 106986448B CN 201710265878 A CN201710265878 A CN 201710265878A CN 106986448 B CN106986448 B CN 106986448B
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water outlet
water
sludge
backwashing
membrane
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CN106986448A (en
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孙楠
侯钦耀
邓晓慧
刘丹彤
李佳瑞
王兴敏
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Northeast Agricultural University
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    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • 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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  • Life Sciences & Earth Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
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  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Separation Using Semi-Permeable Membranes (AREA)
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Abstract

A coupling device of a modified rice hull-ultrafiltration membrane bioreactor and a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water relate to a low-temperature low-turbidity high-color high-ammonia nitrogen source water treatment device and a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water. The invention aims to solve the problems of large occupied area and high treatment cost of the conventional device for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water. The equipment consists of a water inlet system, a coagulation system, a membrane biological reaction system, a water outlet system, a back washing system, a sludge discharge system, a sludge backflow system and an automatic control system; the method comprises the following steps: firstly, starting; secondly, normal water outlet stage; thirdly, backwashing; fourthly, a mud discharging stage; and fifthly, a membrane cleaning stage. The advantages are that: the floor area of the device is reduced, and the cost of unit water treatment is reduced. The invention is mainly used for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water.

Description

Coupling device of modified rice hull-ultrafiltration membrane bioreactor and method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water
Technical Field
The invention relates to a low-temperature low-turbidity high-color high-ammonia nitrogen source water treatment device and a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water.
Background
The Membrane Bioreactor (MBR) has incomparable advantages compared with an active sludge method, such as good removal effect on suspended solid substances, macromolecular organic substances, microorganisms and the like in water, short process flow, small floor area, high sludge concentration, low residual sludge yield, easy realization of full-automatic operation management and the like, but has defects, such as very limited removal capability on microbial metabolites, bacteria, soluble organic substances (DOM) and the like, and easy generation of Membrane pollution, Membrane pollution is a bottleneck restricting popularization and application of the UF-process, and the control method is mainly focused on the aspects of pretreatment of water, negative development of MBR materials, improvement of characteristics of sludge mixed liquor and optimization of operating conditions, wherein the improvement of characteristics of MBR is one of research focus on the pollution of microbial community membranes, the control of characteristics of mixed liquor based on the microbial community, the control of MBR, the improvement of characteristics of mixed liquor, and the optimization of operating conditions, and the problem of the increase of the efficiency of activated carbon particle flocculant added into a system, and the recycling of activated carbon powder, and the like, and the control method is mainly focused on the research of MBR pollution of MBR, the research of MBR, the characteristics of the MBR, the sewage, the research of the sewage, the sewage treatment of the sewage of sewage, the sewage of sewage, the sewage of sewage, the sewage of the.
The existing coagulation-membrane biological reaction process only simply combines coagulation and membrane separation, when the coagulation and membrane biological reactors are respectively two independent units and are combined in a split mode, the occupied area of the device is large, and meanwhile, large flocs formed by coagulation are easy to break when passing through a transmission pipeline, so that the performance of coagulation is influenced; the mixing flocculation effect is not ideal and the coagulant dosage is larger due to the imperfect hydraulic conditions of the mixing stage and the flocculation stage of the coagulation reaction, and simultaneously, the concentration of micro-flocs or colloids which are difficult to coagulate effectively is gradually increased due to the insufficient coagulation effect, so that membrane pollution is easily caused, the membrane flux and the membrane service life are influenced, and a device which can solve the problems does not exist in the prior art.
Disclosure of Invention
The invention aims to solve the problems of large occupied area and high cost of treatment of the conventional device for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water, and provides a modified rice hull-ultrafiltration membrane bioreactor coupling device and a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water.
A modified rice hull-ultrafiltration membrane bioreactor coupling device comprises a water inlet system, a coagulation system, a membrane biological reaction system, a water outlet system, a backwashing system, a sludge discharge system, a sludge backflow system and an automatic control system;
the water inlet system comprises a water inlet pool, a water inlet pump, a water inlet flow meter and a water inlet control valve;
the coagulation system comprises a coagulation tank, a stirrer, a medicine inlet box, a coagulant adding pump and a coagulant flow meter; arranging a stirrer in the coagulation tank;
the membrane biological reaction system comprises a filler adding box, a membrane bioreactor, an ultrafiltration UF membrane component, an aeration pipe, an aeration pump, an overflow pipe, a liquid level controller and filler; the ultrafiltration UF membrane component is arranged in the membrane bioreactor in a hanging manner; the aeration pipe is arranged below the ultrafiltration UF membrane component, and one end of the aeration pipe is connected with an aeration pump;
the water outlet system comprises a water outlet-backwashing shared pressure gauge, a water outlet electromagnetic valve I, a water outlet-backwashing shared water pump, a water outlet electromagnetic valve II, a water outlet flowmeter and a water outlet pool;
the backwashing system comprises a backwashing electromagnetic valve I, a water outlet-backwashing shared water pump, a backwashing electromagnetic valve II, a water outlet-backwashing shared pressure meter and a backwashing flow meter;
the sludge discharge system comprises a sludge pump, a sludge discharge valve and a sludge tank;
the sludge return system comprises a sludge pump and a sludge return valve;
the automatic control system comprises a programmable logic controller, a liquid level controller, a coagulant flow meter, a water outlet-backwashing shared pressure gauge, a water outlet electromagnetic valve I, a water outlet-backwashing shared water pump, a water outlet electromagnetic valve II, a water outlet flow meter, a backwashing electromagnetic valve I, a backwashing electromagnetic valve II, a backwashing flow meter and a water inlet flow meter;
the coagulation tank and the membrane bioreactor are separated by an overflow wall, and the height of the overflow wall is lower than that of other side walls of the coagulation tank and the membrane bioreactor;
the liquid level controller is arranged above the ultrafiltration UF membrane component in a hanging mode, and the height of the tail end of a pointer of the liquid level controller is higher than that of a water outlet of the ultrafiltration UF membrane component and lower than that of an overflow wall;
an overflow port is arranged on the side wall of the non-overflow wall of the membrane bioreactor, the height of the overflow port is lower than that of the overflow wall and higher than that of the tail end of a pointer of a liquid level controller, the overflow port is communicated with one end of an overflow pipe, and the other end of the overflow pipe is communicated with a sludge pool;
discharging sludge generated by the membrane biological reaction system through a sludge discharge system;
the sludge generated by the membrane biological reaction system flows back to enter the coagulation system through the sludge backflow system;
the automatic control system controls the on-off of the water outlet system and the back washing system;
and (3) a normal treatment stage: the backwashing electromagnetic valve I and the backwashing electromagnetic valve II are closed, the water outlet electromagnetic valve I and the water outlet electromagnetic valve II are opened, sewage to be treated enters the coagulation system through the water inlet system and then enters the membrane biological reaction system through overflow, and the treated sewage enters the water outlet system through the membrane biological reaction system;
a backwashing stage: and the water outlet electromagnetic valve I and the water outlet electromagnetic valve II are closed, the backwashing electromagnetic valve I and the backwashing electromagnetic valve II are opened, the treated sewage stored in the water outlet pool sequentially passes through the backwashing electromagnetic valve I, the water outlet-backwashing shared water pump, the backwashing electromagnetic valve II and the backwashing flowmeter, and the ultrafiltration UF membrane assembly is backwashed through a water outlet of the ultrafiltration UF membrane assembly.
A method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water by using a modified rice hull-ultrafiltration membrane bioreactor coupling device is specifically completed according to the following steps:
firstly, a starting stage: taking low-temperature low-turbidity high-color high-ammonia nitrogen source water as sewage to be treated, adding the sewage to be treated into a membrane bioreactor, ensuring that the liquid level of the sewage to be treated is lower than the tail end of a pointer of a liquid level sensor and completely submerging an ultrafiltration UF membrane component, inoculating activated sludge according to the concentration of the activated sludge of 15000 mg/L-20000 mg/L, feeding filler into the membrane bioreactor through a filler feeding box, ensuring that the concentration of suspended solids in the membrane bioreactor is 20000 mg/L-25000 mg/L, starting an aeration pump, carrying out aeration in a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in the membrane bioreactor to be 6 mg/L-7 mg/L; simultaneously starting a water inlet pump, a coagulant adding pump, a stirrer and a programmable logic controller, feeding the sewage to be treated into a coagulation tank from a water inlet tank by the aid of the water inlet pump through a water inlet flow meter and a water inlet control valve in sequence at a feeding amount of 28L/h, feeding the coagulant into the coagulation tank from a coagulant feeding tank through the coagulant flow meter at a feeding amount of 20-25 mg/L, uniformly mixing the coagulant with the stirrer at a rotating speed of 800r/min, and overflowing the coagulated sewage into a membrane bioreactor from the coagulation tank through an overflow wall when the height of the coagulated sewage in the coagulation tank reaches the height of the overflow wall; when liquid in the membrane bioreactor contacts a pointer of a liquid level sensor, a signal is input into a programmable logic controller by the liquid level sensor, the programmable logic controller controls a water outlet electromagnetic valve I, a water outlet-backwashing shared water pump and a water outlet electromagnetic valve II to be opened, the programmable logic controller is utilized to respectively record the adding amount of sewage to be treated and the adding amount of a coagulant according to a water inlet flow meter and a coagulant flow meter, a sludge reflux valve is opened while the water outlet-backwashing shared water pump is started, a sludge pump is started to carry out sludge reflux, the concentration value of sludge in a coagulation tank is controlled to be 500 mg/L-900 mg/L, and the starting stage is ended;
II, normal water outlet stage: continuously feeding the sewage to be treated into a coagulation tank from a water inlet tank by a water inlet pump through a water inlet flow meter and a water inlet control valve in sequence with the addition of 28L/h, continuously feeding the coagulant into a coagulation tank from a coagulant feeding tank by a coagulant feeding pump through the coagulant flow meter with the feeding amount of 10-15 mg/L, controlling the rotating speed of a stirrer to be 800r/min, and keeping the hydraulic retention time in the coagulation tank for 2 min; respectively recording the adding amount of sewage to be treated and the adding amount of a coagulant by using a programmable logic controller according to a water inlet flow meter and a coagulant flow meter, continuously aerating by using an aeration pump in a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in a membrane bioreactor to be 6-7 mg/L; in order to ensure that the concentration of suspended solids in the membrane bioreactor is 20000 mg/L-25000 mg/L, the modified rice hulls are supplemented in time, and the treated sewage passes through a water outlet of an ultrafiltration UF membrane component and sequentially passes through a water outlet electromagnetic valve I, a water outlet-backwashing shared water pump, a water outlet electromagnetic valve II and a water outlet flow meter to enter a water outlet pool; real time of water outlet flowmeterFeeding back the value to the programmable logic controller, and adjusting the frequency of the water outlet-back flushing shared water pump by the programmable logic controller to ensure that the water outlet amount is 130L/m2·h～160L/m2H water out; the hydraulic retention time in the membrane bioreactor is 2 hours;
thirdly, backwashing: according to the feedback information of the water outlet flow meter, when the continuous water outlet time reaches 25-30 min, the programmable logic controller controls the water outlet electromagnetic valve I and the water outlet electromagnetic valve II to be closed, and simultaneously controls the back flush electromagnetic valve I and the back flush electromagnetic valve II to be opened, the treated sewage stored in the water outlet pool sequentially passes through the back flush electromagnetic valve I, the water outlet-back flush common water pump, the back flush electromagnetic valve II and the back flush flow meter, and the ultrafiltration UF membrane module is back flushed through the water outlet of the ultrafiltration UF membrane module; the programmable logic controller sets the back-washing water flow to be 0.4m according to the program3/m2·h～0.5m3/m2H, inputting a signal into a signal input end of the water outlet-backwashing shared water pump, controlling a frequency converter of the water outlet-backwashing shared water pump to adjust the frequency, and ensuring that the flow of the backwashing water is 0.4m3/m2·h～0.5m3/m2H, performing back washing on the ultrafiltration UF membrane component, discharging back washing water into the membrane bioreactor, and discharging the back washing water into a sludge pool through an overflow pipe when the liquid level in the membrane bioreactor reaches the height of an overflow port, wherein the back washing time is controlled to be 2-4 min;
fourthly, a sludge discharge stage: when sludge at the bottom of the membrane bioreactor is accumulated to the bottom pipe wall of the aeration pipe, a sludge pump is used for discharging the sludge to a sludge tank through a sludge discharge valve until the concentration of suspended solids at the bottom of the membrane bioreactor is 20000 mg/L-25000 mg/L;
fifthly, a membrane cleaning stage: when the value of the water outlet-back flush common pressure gauge reaches 0.05MPa, all systems of the modified rice hull-ultrafiltration membrane bioreactor coupling device are closed, and the ultrafiltration UF membrane component is taken out for cleaning.
The invention has the advantages that:
1. the coagulation tank and the membrane bioreactor are designed in an integrated mode, a water outlet-back flush common water pump is adopted, and the floor area of the device is reduced.
2. The front end is provided with a coagulation tank, and a coagulant is added to remove macromolecular organic matters. The problem of large back flush workload due to the attachment of macromolecular organic matters and the like on the surface of the membrane in water is avoided.
3. High-concentration modified rice hull activated carbon is added to form a filter cake layer, so that membrane pollution is reduced, the service life of the membrane is prolonged, and the cost of unit water treatment amount is reduced.
4. A sludge reflux system is arranged, the content of a coagulant is reduced by utilizing the sludge reflux, and the inhibition to organisms is slowed down; and the reduction of the removal effect of the activated sludge on ammonia nitrogen caused by biological inhibition due to the fact that excessive coagulant enters the membrane bioreactor is avoided.
5. The water pump is shared, the water outlet and back flush shared water pump continuously operates during water outlet and back flush, and the loss of the water pump caused by switching on and off during water outlet and back flush is reduced.
6. The ammonia nitrogen removal period and the activated sludge replacement time can be determined and reasonably configured.
Drawings
FIG. 1 is a schematic structural diagram of a modified rice hull-ultrafiltration membrane bioreactor coupling device.
Detailed Description
The first embodiment is as follows: with reference to fig. 1, the embodiment is a modified rice hull-ultrafiltration membrane bioreactor coupling device, which is composed of a water inlet system, a coagulation system, a membrane biological reaction system, a water outlet system, a back washing system, a sludge discharge system, a sludge reflux system and an automatic control system;
the water inlet system comprises a water inlet pool 1, a water inlet pump 2, a water inlet flow meter 3 and a water inlet control valve 4;
the coagulation system comprises a coagulation tank 5, a stirrer 6, a medicine inlet box 7, a coagulant adding pump 8 and a coagulant flow meter 31; a stirrer 6 is arranged in the coagulation tank 5;
the membrane biological reaction system comprises a filler adding box 9, a membrane bioreactor 10, an ultrafiltration UF membrane component 11, an aeration pipe 12, an aeration pump 13, an overflow pipe 14, a liquid level controller 26 and a filler 30; the ultrafiltration UF membrane component 11 is arranged in the membrane bioreactor 10 in a hanging manner; the aeration pipe 12 is arranged below the ultrafiltration UF membrane module 11, and one end of the aeration pipe 12 is connected with an aeration pump 13;
the water outlet system comprises a water outlet-backwashing shared pressure gauge 15, a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18, a water outlet flow meter 19 and a water outlet pool 20;
the backwashing system comprises a backwashing electromagnetic valve I21, a water outlet-backwashing shared water pump 17, a backwashing electromagnetic valve II 22, a water outlet-backwashing shared pressure gauge 15 and a backwashing flow meter 23;
the sludge discharge system comprises a sludge pump 25, a sludge discharge valve 29 and a sludge tank 27;
the sludge return system comprises a sludge pump 25 and a sludge return valve 28;
the automatic control system comprises a programmable logic controller 24, a liquid level controller 26, a coagulant flow meter 31, a water outlet-backwashing shared pressure gauge 15, a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18, a water outlet flow meter 19, a backwashing electromagnetic valve I21, a backwashing electromagnetic valve II 22, a backwashing flow meter 23 and a water inlet flow meter 3;
the coagulation tank 5 and the membrane bioreactor 10 are separated by an overflow wall, and the height of the overflow wall is lower than that of other side walls of the coagulation tank 5 and the membrane bioreactor 10;
the liquid level controller 26 is arranged above the ultrafiltration UF membrane module 11 in a hanging mode, and the height of the tail end of a pointer of the liquid level controller 26 is higher than the height of a water outlet of the ultrafiltration UF membrane module 11 and lower than the height of an overflow wall;
an overflow port is arranged on the side wall of the non-overflow wall of the membrane bioreactor 10, the height of the overflow port is lower than that of the overflow wall and higher than that of the tail end of a pointer of a liquid level controller 26, the overflow port is communicated with one end of an overflow pipe 14, and the other end of the overflow pipe 14 is communicated with a sludge pool 27;
discharging sludge generated by the membrane biological reaction system through a sludge discharge system;
the sludge generated by the membrane biological reaction system flows back to enter the coagulation system through the sludge backflow system;
the automatic control system controls the on-off of the water outlet system and the back washing system;
and (3) a normal treatment stage: the backwashing electromagnetic valve I21 and the backwashing electromagnetic valve II 22 are closed, the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 are opened, sewage to be treated enters the coagulation system through the water inlet system and then enters the membrane biological reaction system through overflow, and the treated sewage enters the water outlet system through the membrane biological reaction system;
a backwashing stage: the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 are closed, the backwashing electromagnetic valve I21 and the backwashing electromagnetic valve II 22 are opened, the treated sewage stored in the water outlet pool 20 passes through the backwashing electromagnetic valve I21, the water outlet-backwashing shared water pump 17, the backwashing electromagnetic valve II 22 and the backwashing flowmeter 23 in sequence, and the ultrafiltration UF membrane assembly 11 is backwashed through a water outlet of the ultrafiltration UF membrane assembly 11.
In the embodiment, the sewage after coagulation in the coagulation tank 5 overflows from the coagulation tank 5 into the membrane bioreactor 10 through the overflow wall.
In the present embodiment, when the liquid in the membrane bioreactor 10 contacts the pointer of the liquid level sensor 26, the signal is input to the programmable logic controller 24 from the liquid level sensor 26, and at this time, the programmable logic controller 24 controls the opening of the water outlet electromagnetic valve i 16, the water outlet-backwashing shared water pump 17 and the water outlet electromagnetic valve ii 18.
The ultrafiltration UF membrane component 11 is a medium polyvinylidene fluoride hollow fiber curtain membrane component, is produced by Tianjin membrane sky science and technology corporation, has the pH range of 2-10, the allowable operation pressure of 0.01-0.05 MPa, the membrane pore diameter of 0.02-0.2 μm, the outer diameter of 400-450 μm, the inner diameter of 320-350 μm, the membrane size of 80cm × 1000, the interception molecular weight of 60000-100000 and the porosity of 40-50%.
FIG. 1 is a schematic structural diagram of a modified rice hull-ultrafiltration membrane bioreactor coupling device, wherein a water inlet pool is shown in FIG. 1; 2 denotes a water inlet pump; 3 denotes a water inflow meter; 4 denotes a water inlet control valve; 5 denotes a coagulation tank; 6 denotes a stirrer; 7 denotes a medicine feeding box; 8 represents a coagulant adding pump; 9 denotes a filler addition tank; 10 denotes a membrane bioreactor; 11 denotes an ultrafiltration UF membrane module; 12 denotes an aeration tube; 13 denotes an aeration pump; 14 denotes an overflow tube; 15 represents a water outlet-back flushing common pressure gauge; 16 represents a water outlet electromagnetic valve I; 17 represents a water outlet-backwashing shared water pump; 18 represents a water outlet electromagnetic valve II; 19, a water flow meter; 20 denotes a water outlet tank; 21 denotes a backwash solenoid valve i; 22 denotes a backwash solenoid valve ii; 23 denotes a backwash flow meter; 24 denotes a programmable logic controller; 25 denotes a sludge pump; 26 denotes a liquid level controller; 27 denotes a sludge tank; 28 denotes a sludge return valve; 29 denotes a sludge discharge valve; 30 represents a filler; and 31 denotes a coagulant flow meter.
The invention tries to add high-concentration modified rice hulls into UF-MBR to form a modified rice hull-UF-MBR combined process, researches the decontamination effect of a UF-MBR and a modified rice hull-UF-MBR parallel system on low-temperature high-color high-ammonia nitrogen source water, the performance of activated sludge in a reactor and the membrane pollution condition, inspects the action mechanism and the efficiency of the modified rice hulls, explores a new method for treating the low-temperature high-color high-ammonia nitrogen source water or effectively relieving the membrane pollution of the MBR, and provides technical support for the popularization and the application of the modified rice hull-UF-MBR.
The rice hull contains 15-20% of amorphous hydrated silicon dioxide and other main components of hydrocarbon. The rice hulls have the characteristics of large silicon content, small porous capacity, rough texture and the like, the produced activated carbon has strong adsorption capacity on various organic compounds, does not contain harmful impurities (such as lead and arsenic), can be used for various industries such as water treatment and the like, has huge market potential, is sufficient in rice hull raw materials and low in price, and the produced activated carbon product has low cost, not only saves energy, but also realizes waste recycling, meets the sustainable development requirement, and has great practical value and application prospect.
The feasibility of the modified rice hull-UF-MBR combined process is verified based on the membrane pollution slowing principle: the modified rice hull-UF-MBR combined process integrates the strong adsorption effect of the modified rice hulls, the biodegradation effect of the MBR and the high-efficiency interception effect of a membrane, wherein the rice hull-based activated carbon has a huge specific surface area and a developed pore structure, is easy to adsorb and enrich organic matters, and is also a good carrier for the attachment and growth of microorganisms, so that the whole system has high biological activity and strong stability; the modified rice hulls adsorb extracellular polymers of partial microorganisms, and a filter cake layer is formed on the surface of the membrane, so that membrane pollution and the growth speed of transmembrane pressure difference (TMP) can be effectively slowed down, and the membrane module is protected. Therefore, the addition of the modified rice hulls can improve the performance of activated sludge in the reactor, increase the water permeability of the membrane, effectively slow down membrane pollution, improve the effluent quality of the UF-MBR system, ensure that the removal efficiency of pollutants is more stable and reliable, and improve the impact load resistance of the system.
The precipitated sludge in the membrane bioreactor 10 flows back to the coagulation tank 5, so that the coagulation effect of low-turbidity water can be improved; in addition, the modified rice hulls which adsorb a large amount of ammonia nitrogen and organic matters can be used as fertilizers, and the utilization of renewable resources is the development trend of the current environment-friendly high-tech technology; 6500 million tons of straws and 8000 million tons of livestock and poultry manure (which are important reasons for causing high-color high-ammonia-nitrogen water quality) generated in rural areas of Heilongjiang province every year need to be effectively treated.
The second embodiment is as follows: with reference to fig. 1, the present embodiment differs from the first embodiment in that: the sewage to be treated is stored in the water inlet tank 1, and is sent into the coagulation tank 5 through the water inlet flow meter 3 and the water inlet control valve 4 by the water inlet pump 2. The rest is the same as the first embodiment.
The third concrete implementation mode: referring to fig. 1, the difference between this embodiment and the first or second embodiment is: the coagulant is stored in the coagulant tank 7, and the coagulant is fed into the coagulation tank 5 through the coagulant flow meter 31 by the coagulant feed pump 8. The others are the same as in the first or second embodiment.
The fourth concrete implementation mode: with reference to fig. 1, the difference between this embodiment and one of the first to third embodiments is: the filler 30 is stored in the filler adding box 9, and the filler 30 is added into the membrane bioreactor 10 through the filler adding box 9. The others are the same as the first to third embodiments.
The fifth concrete implementation mode: with reference to fig. 1, the difference between this embodiment and one of the first to fourth embodiments is: the sludge outlet at the bottom of the membrane bioreactor 10 is communicated with a sludge tank 27 through a sludge pump 25 and a sludge discharge valve 29, and the sludge outlet at the bottom of the membrane bioreactor 10 is communicated with the coagulation tank 5 through the sludge pump 25 and a sludge return valve 28. The rest is the same as the first to fourth embodiments.
Sixth embodiment, referring to fig. 1, the difference between this embodiment and the first to fifth embodiments is that the UF membrane module 11 is a pvdf hollow fiber curtain membrane module having a pH range of 2 to 10, an allowable operating pressure of 0.01 to 0.05MPa, a membrane pore diameter of 0.02 to 0.2 μm, an outer diameter of 400 to 450 μm, an inner diameter of 320 to 350 μm, a membrane size of 80cm × 1000, a molecular weight cut-off of 60000 to 100000, and a porosity of 40 to 50%, and the others are the same as those of the first to fifth embodiments.
The seventh embodiment: with reference to fig. 1, the embodiment is a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water by using a modified rice hull-ultrafiltration membrane bioreactor coupling device, and is characterized by comprising the following steps:
firstly, a starting stage: taking low-temperature low-turbidity high-color high-ammonia nitrogen source water as sewage to be treated, adding the sewage to be treated into a membrane bioreactor 10, ensuring that the liquid level of the sewage to be treated is lower than the tail end of a pointer of a liquid level sensor 26 and completely submerging an ultrafiltration UF membrane component 11, inoculating activated sludge according to the concentration of the activated sludge of 15000 mg/L-20000 mg/L, feeding a filler 30 into the membrane bioreactor 10 through a filler feeding box 9, ensuring that the concentration of suspended solids in the membrane bioreactor 10 is 20000 mg/L-25000 mg/L, starting an aeration pump 13, carrying out aeration by adopting a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in the membrane bioreactor 10 to be 6 mg/L-7 mg/L; simultaneously starting a water inlet pump 2, a coagulant adding pump 8, a stirrer 6 and a programmable logic controller 24, feeding the sewage to be treated into a coagulation tank 5 from a water inlet tank 1 by the aid of the water inlet pump 2 and sequentially passing through a water inlet flow meter 3 and a water inlet control valve 4 at a feeding amount of 28L/h, feeding the coagulant into the coagulation tank 5 from a coagulant feeding box 7 by the aid of the coagulant adding pump 8 and passing through a coagulant flow meter 31 at a feeding amount of 20 mg/L-25 mg/L, uniformly mixing at a rotating speed of 800r/min by the aid of the stirrer 6, and when the sewage after coagulation in the coagulation tank 5 reaches the height of an overflow wall, performing membrane biological entry on the coagulated sewage from the coagulation tank 5 into the reactor 10 through the overflow wall; when liquid in the membrane bioreactor 10 contacts a pointer of a liquid level sensor 26, a signal is input into a programmable logic controller 24 through the liquid level sensor 26, at the moment, the programmable logic controller 24 controls a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17 and a water outlet electromagnetic valve II 18 to be opened, the addition amount of sewage to be treated and the addition amount of a coagulant are respectively recorded by the programmable logic controller 24 according to a water inlet flow meter 3 and a coagulant flow meter 31, a sludge reflux valve 28 is opened while the water outlet-backwashing shared water pump 17 is started, a sludge pump 25 is started to carry out sludge reflux, the concentration value of sludge in a coagulation tank 5 is controlled to be 500 mg/L-900 mg/L, and the starting stage is ended;
II, normal water outlet stage: continuously feeding the sewage to be treated into a coagulation tank 5 from a water inlet tank 1 by a water inlet pump 2 through a water inlet flow meter 3 and a water inlet control valve 4 in sequence with the addition amount of 28L/h, continuously feeding a coagulant into the coagulation tank 5 from a medicine feeding box 7 by a coagulant feeding pump 8, feeding the coagulant into the coagulation tank 5 through a coagulant flow meter 31 with the feeding amount of 10-15 mg/L, controlling the rotating speed of a stirrer 6 to be 800r/min, and keeping the hydraulic retention time in the coagulation tank 5 to be 2 min; the addition amount of sewage to be treated and the addition amount of a coagulant are respectively recorded by a programmable logic controller 24 according to a water inlet flow meter 3 and a coagulant flow meter 31, an aeration pump 13 continuously aerates in a continuous aeration mode, and the concentration of dissolved oxygen in liquid in a membrane bioreactor 10 is controlled to be 6 mg/L-7 mg/L; in order to ensure that the concentration of suspended solids in the membrane bioreactor 10 is 20000 mg/L-25000 mg/L, the filler 30 is supplemented in time, and the treated sewage passes through a water outlet of the ultrafiltration UF membrane component 11, and sequentially passes through a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18 and a water outlet flow meter 19 to enter a water outlet pool 20; the water outlet flow meter 19 feeds back the value to the programmable logic controller 24 at any time, and the programmable logic controller 24 adjusts the frequency of the water outlet-backwashing shared water pump 17 to ensure that the water outlet quantity is 130L/m2·h～160L/m2H water out; the hydraulic retention time in the membrane bioreactor 10 is 2 hours;
thirdly, backwashing: according to the feedback information of the water outlet flowmeter 19, when the continuous water outlet time reaches 25 min-30 min, the programmable logic controller 24 controls the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 to be closed, and controls the backwashing electromagnetic valve I21 and the backwashing electromagnetic valve II 22 to be openedStarting, the treated sewage stored in the water outlet pool 20 passes through a backwashing electromagnetic valve I21, a water outlet-backwashing shared water pump 17, a backwashing electromagnetic valve II 22 and a backwashing flowmeter 23 in sequence, and the ultrafiltration UF membrane module 11 is backwashed through a water outlet of the ultrafiltration UF membrane module 11; the programmable logic controller 24 sets the back-wash water flow rate to 0.4m according to the program3/m2·h～0.5m3/m2H, inputting a signal into a signal input end of the water outlet-backwashing shared water pump 17, controlling a frequency converter of the water outlet-backwashing shared water pump 17 to adjust the frequency, and ensuring that the flow of the backwashing water is 0.4m3/m2·h～0.5m3/m2H, backwashing the ultrafiltration UF membrane component 11, discharging backwashing water into the membrane bioreactor 10, and discharging the backwashing water into a sludge tank 27 through an overflow pipe 14 when the liquid level in the membrane bioreactor 10 reaches the height of an overflow port, wherein the backwashing time is controlled to be 2-4 min;
fourthly, a sludge discharge stage: when sludge at the bottom of the membrane bioreactor 10 is accumulated to the bottom pipe wall of the aeration pipe 12, the sludge is discharged to a sludge tank 27 by a sludge pump 25 through a sludge discharge valve 29 until the concentration of suspended solids at the bottom of the membrane bioreactor 10 is 20000 mg/L-25000 mg/L;
fifthly, a membrane cleaning stage: when the value of the water outlet-back flush common pressure gauge 15 reaches 0.05MPa, all systems of the modified rice hull-ultrafiltration membrane bioreactor coupling device are closed, and the ultrafiltration UF membrane component 11 is taken out for cleaning.
The specific implementation mode is eight: the seventh embodiment is different from the seventh embodiment in that: in the second step, the organic carbon source is added into the membrane bioreactor 10 periodically to ensure the COD of the liquid in the membrane bioreactor 10Mn5 mg/L-7 mg/L, TOC6 mg-8 mg/L, pH 7. The rest is the same as the seventh embodiment.
The specific implementation method nine: the seventh or eighth embodiment differs from the first embodiment in that: in the step one, the filler 30 is modified rice hull activated carbon. The others are the same as the seventh or eighth embodiments.
The detailed implementation mode is ten: the present embodiment differs from the ninth embodiment in that: the modified rice hull activated carbon is obtained according to the following steps: rice huskRemoving impurities, washing with water, soaking in 1mol/LHCl solution for 4h, washing with water until pH is 7-8, drying at 100 deg.C, and removing K+、Na+、Ca2+、Fe2+、Mg2+And putting the dried rice hulls into a muffle furnace to isolate air, carbonizing for 3h at 800 ℃, heating and refluxing 0.2g of carbonized rice hulls and 20mL of 1.5mol/L NaOH solution for 2h, filtering, obtaining filter residues, washing the filter residues with water until the pH value is 7-8, drying to obtain modified rice hull activated carbon primary products, and activating at the high temperature of 600 ℃ to obtain the modified rice hull activated carbon. The rest is the same as in the ninth embodiment.
The concrete implementation mode eleven: the seventh to tenth embodiments are different from the first to seventh embodiments in that: the activated sludge in the first step is obtained according to the following steps: taking return sludge from a secondary sedimentation tank of a sewage plant, and obtaining activated sludge after acclimation and maturation. The rest is the same as the seventh to tenth embodiments.
The following tests were carried out to confirm the effects of the present invention
Example 1: referring to fig. 1, a modified rice hull-ultrafiltration membrane bioreactor coupling device comprises a water inlet system, a coagulation system, a membrane biological reaction system, a water outlet system, a backwashing system, a sludge discharge system, a sludge reflux system and an automatic control system;
the water inlet system comprises a water inlet pool 1, a water inlet pump 2, a water inlet flow meter 3 and a water inlet control valve 4;
the coagulation system comprises a coagulation tank 5, a stirrer 6, a medicine inlet box 7, a coagulant adding pump 8 and a coagulant flow meter 31; a stirrer 6 is arranged in the coagulation tank 5;
the membrane biological reaction system comprises a filler adding box 9, a membrane bioreactor 10, an ultrafiltration UF membrane component 11, an aeration pipe 12, an aeration pump 13, an overflow pipe 14, a liquid level controller 26 and a filler 30; the ultrafiltration UF membrane component 11 is arranged in the membrane bioreactor 10 in a hanging manner; the aeration pipe 12 is arranged below the ultrafiltration UF membrane module 11, and one end of the aeration pipe 12 is connected with an aeration pump 13;
the water outlet system comprises a water outlet-backwashing shared pressure gauge 15, a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18, a water outlet flow meter 19 and a water outlet pool 20;
the backwashing system comprises a backwashing electromagnetic valve I21, a water outlet-backwashing shared water pump 17, a backwashing electromagnetic valve II 22, a water outlet-backwashing shared pressure gauge 15 and a backwashing flow meter 23;
the sludge discharge system comprises a sludge pump 25, a sludge discharge valve 29 and a sludge tank 27;
the sludge return system comprises a sludge pump 25 and a sludge return valve 28;
the automatic control system comprises a programmable logic controller 24, a liquid level controller 26, a coagulant flow meter 31, a water outlet-backwashing shared pressure gauge 15, a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18, a water outlet flow meter 19, a backwashing electromagnetic valve I21, a backwashing electromagnetic valve II 22, a backwashing flow meter 23 and a water inlet flow meter 3;
the coagulation tank 5 and the membrane bioreactor 10 are separated by an overflow wall, and the height of the overflow wall is lower than that of other side walls of the coagulation tank 5 and the membrane bioreactor 10;
the liquid level controller 26 is arranged above the ultrafiltration UF membrane module 11 in a hanging mode, and the height of the tail end of a pointer of the liquid level controller 26 is higher than the height of a water outlet of the ultrafiltration UF membrane module 11 and lower than the height of an overflow wall;
an overflow port is arranged on the side wall of the non-overflow wall of the membrane bioreactor 10, the height of the overflow port is lower than that of the overflow wall and higher than that of the tail end of a pointer of a liquid level controller 26, the overflow port is communicated with one end of an overflow pipe 14, and the other end of the overflow pipe 14 is communicated with a sludge pool 27;
discharging sludge generated by the membrane biological reaction system through a sludge discharge system; the sludge generated by the membrane biological reaction system flows back to enter the coagulation system through the sludge backflow system; the automatic control system controls the on-off of the water outlet system and the back washing system;
the coagulant is stored in the coagulant tank 7, and the coagulant is fed into the coagulation tank 5 through the coagulant flow meter 31 by the coagulant feed pump 8.
The filler 30 is stored in the filler adding box 9, and the filler 30 is added into the membrane bioreactor 10 through the filler adding box 9.
When liquid in the membrane bioreactor 10 contacts a pointer of the liquid level sensor 26, a signal is input into the programmable logic controller 24 through the liquid level sensor 26, and at the moment, the programmable logic controller 24 controls the opening of the water outlet electromagnetic valve I16, the water outlet-backwashing shared water pump 17 and the water outlet electromagnetic valve II 18.
The sludge outlet at the bottom of the membrane bioreactor 10 is communicated with a sludge tank 27 through a sludge pump 25 and a sludge discharge valve 29, and the sludge outlet at the bottom of the membrane bioreactor 10 is communicated with the coagulation tank 5 through the sludge pump 25 and a sludge return valve 28.
The treated sewage passes through a water outlet of the ultrafiltration UF membrane component 11 and then sequentially passes through a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18 and a water outlet flow meter 19 to enter a water outlet pool 20.
The ultrafiltration UF membrane component 11 is a medium polyvinylidene fluoride hollow fiber curtain type membrane component, the pH range is 2-10, the allowable operating pressure is 0.01-0.05 MPa, the membrane aperture is 0.02-0.2 μm, the outer diameter is 400-450 μm, the inner diameter is 320-350 μm, the membrane size is 80cm × 1000, the molecular weight cut-off is 60000-100000, and the porosity is 40-50%.
And (3) a normal treatment stage: the backwashing electromagnetic valve I21 and the backwashing electromagnetic valve II 22 are closed, the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 are opened, the sewage to be treated is stored in the water inlet pool 1, and the water inlet pump 2 is utilized to send the sewage to be treated into the coagulation pool 5 through the water inlet flow meter 3 and the water inlet control valve 4; the sewage after coagulation in the coagulation tank 5 overflows from the coagulation tank 5 into the membrane bioreactor 10 through the overflow wall; the treated sewage passes through a water outlet of the ultrafiltration UF membrane component 11 and then sequentially passes through a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18 and a water outlet flow meter 19 to enter a water outlet pool 20.
A backwashing stage: the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 are closed, the backwashing electromagnetic valve I21 and the backwashing electromagnetic valve II 22 are opened, the treated sewage stored in the water outlet pool 20 passes through the backwashing electromagnetic valve I21, the water outlet-backwashing shared water pump 17, the backwashing electromagnetic valve II 22 and the backwashing flowmeter 23 in sequence, and the ultrafiltration UF membrane assembly 11 is backwashed through a water outlet of the ultrafiltration UF membrane assembly 11.
Example 2: with reference to fig. 1, a method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water by using a modified rice hull-ultrafiltration membrane bioreactor coupling device is specifically completed according to the following steps:
firstly, a starting stage: taking low-temperature low-turbidity high-color high-ammonia nitrogen source water as sewage to be treated, adding the sewage to be treated into a membrane bioreactor 10, ensuring that the liquid level of the sewage to be treated is lower than the tail end of a pointer of a liquid level sensor 26 and completely submerging an ultrafiltration UF membrane component 11, inoculating activated sludge according to the concentration of the activated sludge of 15000 mg/L-20000 mg/L, feeding a filler 30 into the membrane bioreactor 10 through a filler feeding box 9, ensuring that the concentration of suspended solids in the membrane bioreactor 10 is 20000 mg/L-25000 mg/L, starting an aeration pump 13, carrying out aeration by adopting a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in the membrane bioreactor 10 to be 6 mg/L-7 mg/L; simultaneously starting a water inlet pump 2, a coagulant adding pump 8, a stirrer 6 and a programmable logic controller 24, feeding the sewage to be treated into a coagulation tank 5 from a water inlet tank 1 by using the water inlet pump 2 and sequentially passing through a water inlet flow meter 3 and a water inlet control valve 4 with the addition of 28L/h, continuously adding the coagulant into the coagulation tank 5 from a medicine feeding box 7 by using the coagulant adding pump 8, feeding the coagulant into the coagulation tank 5 through a coagulant flow meter 31 with the addition of 20 mg/L-25 mg/L, uniformly mixing at the rotating speed of 800r/min by using the stirrer 6, and when the coagulated sewage in the coagulation tank 5 reaches the height of an overflow wall, overflowing the coagulated sewage from the coagulation tank 5 into a membrane bioreactor 10 through the overflow wall, wherein the coagulated sewage contains micro floccules; when liquid in the membrane bioreactor 10 contacts a pointer of a liquid level sensor 26, a signal is input into a programmable logic controller 24 through the liquid level sensor 26, at the moment, the programmable logic controller 24 controls a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17 and a water outlet electromagnetic valve II 18 to be opened, the addition amount of sewage to be treated and the addition amount of a coagulant are respectively recorded by the programmable logic controller 24 according to a water inlet flow meter 3 and a coagulant flow meter 31, a sludge reflux valve 28 is opened while the water outlet-backwashing shared water pump 17 is started, a sludge pump 25 is started to carry out sludge reflux, the concentration value of sludge in a coagulation tank 5 is controlled to be 500 mg/L-900 mg/L, and the starting stage is ended;
II, normal water outlet stage: continuously feeding the sewage to be treated into a coagulation tank 5 from a water inlet tank 1 by a water inlet pump 2 through a water inlet flow meter 3 and a water inlet control valve 4 in sequence with the addition of 28L/h, continuously feeding a coagulant into a coagulation tank 5 from a coagulant feeding tank 7 by a coagulant feeding pump 8 through a coagulant flow meter 31 with the addition of 10 mg/L-15 mg/L, controlling the rotating speed of a stirrer 6 to be 800r/min, and keeping the hydraulic retention time in the coagulation tank 5 for 2 min; the addition amount of sewage to be treated and the addition amount of a coagulant are respectively recorded by a programmable logic controller 24 according to a water inlet flow meter 3 and a coagulant flow meter 31, an aeration pump 13 continuously aerates in a continuous aeration mode, and the concentration of dissolved oxygen in liquid in a membrane bioreactor 10 is controlled to be 6 mg/L-7 mg/L; the disturbance of the bubbles enables the membrane biological reaction zone to form micro vortex, prevents flocs from sinking, is beneficial to mutual collision and flocculation of the flocs, further realizes full adsorption of pollutants, provides rich dissolved oxygen by aeration, is beneficial to growth and reproduction of microorganisms, and performs biodegradation to improve the effect of water treatment; in order to ensure that the concentration of suspended solids in the membrane bioreactor 10 is 20000 mg/L-25000 mg/L, the filler 30 is supplemented in time, and the treated sewage passes through a water outlet of the ultrafiltration UF membrane component 11, and sequentially passes through a water outlet electromagnetic valve I16, a water outlet-backwashing shared water pump 17, a water outlet electromagnetic valve II 18 and a water outlet flow meter 19 to enter a water outlet pool 20; the water outlet flow meter 19 feeds back the value to the programmable logic controller 24 at any time, and the programmable logic controller 24 adjusts the frequency of the water outlet-backwashing shared water pump 17 to ensure that the water outlet quantity is 130L/m2·h～160L/m2H water out; the hydraulic retention time in the membrane bioreactor 10 is 2 hours;
thirdly, backwashing: according to the feedback information of the water outlet flowmeter 19, when the continuous water outlet time reaches 25-30 min, the programmable logic controller 24 controls the water outlet electromagnetic valve I16 and the water outlet electromagnetic valve II 18 to be closed, and simultaneously controls the back flush electromagnetic valve I21 and the back flush electromagnetic valve II 22 to be opened, the treated sewage stored in the water outlet pool 20 passes through the back flush electromagnetic valve I21, the water outlet-back flush shared water pump 17, the back flush electromagnetic valve II 22 and the back flush flowmeter 23 in sequence, and the ultrafiltration UF membrane component 11 is subjected to ultrafiltration through the water outlet thereofBackwashing the UF membrane module 11; the programmable logic controller 24 sets the back-wash water flow rate to 0.4m according to the program3/m2·h～0.5m3/m2H, inputting a signal into a signal input end of the water outlet-backwashing shared water pump 17, controlling a frequency converter of the water outlet-backwashing shared water pump 17 to adjust the frequency, and ensuring that the flow of the backwashing water is 0.4m3/m2·h～0.5m3/m2H, backwashing the ultrafiltration UF membrane component 11, discharging backwashing water into the membrane bioreactor 10, and discharging the backwashing water into a sludge tank 27 through an overflow pipe 14 when the liquid level in the membrane bioreactor 10 reaches the height of an overflow port, wherein the backwashing time is controlled to be 2-4 min;
fourthly, a sludge discharge stage: when sludge at the bottom of the membrane bioreactor 10 is accumulated to the bottom pipe wall of the aeration pipe 12, the sludge is discharged to a sludge tank 27 by a sludge pump 25 through a sludge discharge valve 29 until the concentration of suspended solids at the bottom of the membrane bioreactor 10 is 20000 mg/L-25000 mg/L;
fifthly, a membrane cleaning stage: when the value of the water outlet-back flush common pressure gauge 15 reaches 0.05MPa, all systems of the modified rice hull-ultrafiltration membrane bioreactor coupling device are closed, and the ultrafiltration UF membrane component 11 is taken out for cleaning.
In the second step of this embodiment, an organic carbon source is periodically added to the membrane bioreactor 10 to ensure the COD of the liquid in the membrane bioreactor 10Mn5mg/L～7mg/L，TOC 6mg/L～8mg/L，pH＝7。
In the first step of this embodiment, the filler 30 is modified rice hull activated carbon; the modified rice hull activated carbon is obtained according to the following steps: removing impurities from rice hulls, washing with water, soaking in 1mol/L HCl solution for 4h, washing with water until the pH value is 7-8, drying at 100 ℃, and removing K+、Na+、Ca2+、Fe2+、Mg2+And putting the dried rice hulls into a muffle furnace to isolate air, carbonizing for 3h at 800 ℃, heating and refluxing 0.2g of carbonized rice hulls and 20mL of 1.5mol/L NaOH solution for 2h, filtering, obtaining filter residues, washing the filter residues with water until the pH value is 7-8, drying to obtain modified rice hull activated carbon primary products, and activating at the high temperature of 600 ℃ to obtain the modified rice hull activated carbon.
In the first step of this embodiment, the activated sludge is obtained by the following steps: taking return sludge from a secondary sedimentation tank of a sewage plant, and obtaining activated sludge after acclimation and maturation.
The modified rice husk has the following effects: the relative molecular weight distribution of organic matters in the sludge mixed liquid of the coupling device of the membrane bioreactor and the modified rice husk-membrane bioreactor is continuously measured, and the result shows that the modified rice husk increases the system pair of the sludge mixed liquid of 3K-10 KD, 10K-100 KD,>100KD three-interval organic matter (using UV)254Value representation), which is respectively improved by 3%, 12% and 4% compared with a single membrane bioreactor, shows that the modified rice hulls adsorb partial organic matters and microbial metabolites in the sludge mixed solution, and in addition, sludge flocs added with the modified rice hulls are mutually aggregated and bonded to form biological rice hulls, thereby providing excellent living environment for microorganisms, enhancing the sludge activity and enabling the biological rice hulls to have stronger degradation capacity on the organic matters.
The modified rice hull-ultrafiltration membrane bioreactor coupling device provided by the embodiment is provided by the embodiment 1.
The characteristics of the low-temperature low-turbidity high-color high-ammonia nitrogen source water are as follows: the water temperature is 0-5 ℃, the turbidity is 10 NTU-15 NTU, the chroma is 40-50 ℃, and the ammonia nitrogen is higher than 1 mg/L-1.5 mg/L.
The addition of the biodegradable organic carbon source (glucose) can ensure that the growth and the propagation of microorganisms in the mixed liquid of the reactor are not limited by poor nutrition environment, promote the biodegradable organic matters and the difficultly biodegradable organic matters accumulated in the reactor to generate the co-metabolism effect, explore the potential of the activated sludge and ensure the COD of the liquid in the membrane bioreactor 10Mn5mg/L～7mg/L，TOC6mg/L～8mg/L，pH＝7。
The operation is carried out for 3 days, the chroma of the inlet water is stabilized at 50 ℃, the chroma of the outlet water is 2-3 ℃, and the removal rate is about 96%; CODMnThe content is 2.5 mg/L-2.2 mg/L, and the removal rate reaches 70% -80%; NH (NH)4The removal rate of-N is relatively high at the beginning, about 95%, and the removal rate of the total nitrogen content in water is low, 20% -26%.
The chroma of the effluent after the treatment for 9 days is 3-5 ℃; the chroma removal rate is 90-95 percent; CODMnThe removal rate is 40 to 48 percent, and the content is about 2mg/L, butThe removal rate is suddenly reduced to about 40 percent due to the fact that water is changed after the ninth day; NH (NH)4The removal rate of N is reduced to 77-85%, the removal rate of the total nitrogen content in water is 19-29%, and the total nitrogen content in the effluent is 3.3-5.1 mg/L.
After the treatment for 15 days, the chroma of the water is stabilized at about 40 ℃, and the chroma of the water is 0-4 ℃; COD of effluentMn1.62mg/L to 1.85mg/L, the removal rate is 70 percent to 75 percent, and NH in water4N is 1mg/L to 1.5mg/L, the removal rate is 80 percent to 88 percent, the total nitrogen content in water is 2.2mg/L to 2.8mg/L, and the removal rate is 15 percent to 30 percent.
After the operation is carried out for 30 days, the chroma of the inlet water is improved to 40-45 ℃, and the chroma of the outlet water is 1-2 ℃; CODMnThe removal rate is close to 88 percent, and the effluent CODMnThe value is stabilized at about 1.5 mg/L; NH in water4The removal rate of-N is basically about 95 percent of that of three days before test operation, the total ammonia content in water is gradually reduced, and the removal rate is about 25 to 40 percent.
After the operation is carried out for 45 days, the removal rate of the effluent chromaticity reaches 94-98 percent, and the effluent chromaticity is relatively stable at about 2 ℃; CODMnThe removal rate is 80% -90%; NH in water4The removal rate of-N fluctuates stably, the average is about 95%, and the removal rate of the total nitrogen content is 35-50%.
The operation is carried out for 90 days, the chroma of the inlet water is stabilized at about 37 ℃, the chroma of the outlet water is close to 0, and the chroma removal rate is close to 98-100%; CODMnThe removal rate fluctuates stably, and the average is 85 percent; NH in water4The removal rate of N fluctuates stably, and the average is 96.2 to 98 percent; the total nitrogen content in the effluent is stabilized at 0.7-0.9 mg/L, and the removal rate reaches 59% -70%.

Claims (7)

1. A method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water by using a modified rice hull-ultrafiltration membrane bioreactor coupling device is characterized by comprising the following steps of:
firstly, a starting stage: taking low-temperature low-turbidity high-color high-ammonia nitrogen source water as sewage to be treated, adding the sewage to be treated into a membrane bioreactor (10), ensuring that the liquid level of the sewage to be treated is lower than the tail end of a pointer of a liquid level sensor (26) and completely submerging an ultrafiltration UF membrane component (11), then inoculating activated sludge according to the concentration of the activated sludge of 15000 mg/L-20000 mg/L, adding a filler (30) into the membrane bioreactor (10) through a filler adding box (9), ensuring that the concentration of suspended solids in the membrane bioreactor (10) is 20000 mg/L-25000 mg/L, starting an aeration pump (13), carrying out aeration by adopting a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in the membrane bioreactor (10) to be 6 mg/L-7 mg/L; simultaneously starting a water inlet pump (2), a coagulant adding pump (8), a stirrer (6) and a programmable logic controller (24), feeding the sewage to be treated into a coagulation tank (5) from a water inlet tank (1) by using the water inlet pump (2) and sequentially passing through a water inlet flow meter (3) and a water inlet control valve (4) with the addition of 28L/h, feeding the coagulant into the coagulation tank (5) from a medicine inlet tank (7) by using the coagulant adding pump (8) and passing through a coagulant flow meter (31) with the addition of 20 mg/L-25 mg/L, uniformly mixing at the rotating speed of 800r/min by using the stirrer (6), and when the sewage coagulated in the coagulation tank (5) reaches the height of an overflow wall, feeding the coagulated sewage into a membrane bioreactor (10) from the coagulation tank (5) through the overflow wall; when liquid in the membrane bioreactor (10) contacts a pointer of a liquid level sensor (26), a signal is input into a programmable logic controller (24) through the liquid level sensor (26), the programmable logic controller (24) controls a water outlet electromagnetic valve I (16), a water outlet-backwashing shared water pump (17) and a water outlet electromagnetic valve II (18) to be opened, the addition amount of sewage to be treated and the addition amount of a coagulant are respectively recorded by the programmable logic controller (24) according to a water inlet flow meter (3) and a coagulant flow meter (31), a sludge reflux valve (28) is opened while the water outlet-backwashing shared water pump (17) is started, a sludge pump (25) is started to reflux sludge, the concentration value of the sludge in a coagulation tank (5) is controlled to be 500 mg/L-900 mg/L, and the starting stage is ended;
in the first step, the filler (30) is modified rice hull activated carbon, and the modified rice hull activated carbon is obtained by the following steps: removing impurities from rice hulls, washing with water, soaking in 1mol/L HCl solution for 4h, washing with water until the pH value is 7-8, drying at 100 ℃, and removing K+、Na+、Ca2+、Fe2+、Mg2+The dried rice husk is put into a muffle furnace to isolate air 8Carbonizing at 00 ℃ for 3h, heating and refluxing 0.2g of carbonized rice hulls and 20mL of 1.5mol/L NaOH solution for 2h, filtering, obtaining filter residues, washing the filter residues with water until the pH value is 7-8, drying to obtain modified rice hull activated carbon primary products, and activating at 600 ℃ to obtain modified rice hull activated carbon;
II, normal water outlet stage: continuously feeding the sewage to be treated into a coagulation tank (5) from a water inlet tank (1) by a water inlet pump (2) through a water inlet flow meter (3) and a water inlet control valve (4) in sequence with the addition of 28L/h, continuously feeding a coagulant into the coagulation tank (5) from a coagulant feeding box (7) by a coagulant feeding pump (8) through a coagulant flow meter (31) with the addition of 10 mg/L-15 mg/L, controlling the rotating speed of a stirrer (6) to be 800r/min, and keeping the hydraulic retention time in the coagulation tank (5) to be 2 min; recording the addition amount of sewage to be treated and the addition amount of a coagulant by using a programmable logic controller (24) according to a water inlet flow meter (3) and a coagulant flow meter (31), continuously aerating by using an aeration pump (13) in a continuous aeration mode, and controlling the concentration of dissolved oxygen in liquid in a membrane bioreactor (10) to be 6-7 mg/L; in order to ensure that the concentration of suspended solids in the membrane bioreactor (10) is 20000 mg/L-25000 mg/L, the filler (30) is supplemented in time, and the treated sewage passes through a water outlet of an ultrafiltration UF membrane component (11), and sequentially passes through a water outlet electromagnetic valve I (16), a water outlet-backwashing shared water pump (17), a water outlet electromagnetic valve II (18) and a water outlet flow meter (19) to enter a water outlet pool (20); the water outlet flow meter (19) feeds back the value to the programmable logic controller (24) at any time, and the frequency of the water outlet-back flushing shared water pump (17) is adjusted by the programmable logic controller (24) to ensure that the water outlet quantity is 130L/m2·h~160L/m2H water out; the hydraulic retention time in the membrane bioreactor (10) is 2 h;
in the second step, an organic carbon source is periodically added into the membrane bioreactor (10) to ensure the COD of the liquid in the membrane bioreactor (10)Mn5mg/L~7mg/L，TOC 6mg/L~8mg/L，pH=7；
Thirdly, backwashing: according to the feedback information of the water outlet flowmeter (19), when the continuous water outlet time reaches 25-30 min, the programmable logic controller (24) controls the water outlet electromagnetic valve I (16) and the water outlet electromagnetic valve II (18) to be closed, and simultaneously controls the backwashing electromagnetic valve I (21) and the backwashing electromagnetic valve II (22) to be opened, and the water outlet pool (20) is stored for treatment and then is subjected to treatmentSewage sequentially passes through a backwashing electromagnetic valve I (21), a water outlet-backwashing common water pump (17), a backwashing electromagnetic valve II (22) and a backwashing flowmeter (23), and the ultrafiltration UF membrane module (11) is backwashed through a water outlet of the ultrafiltration UF membrane module (11); the programmable logic controller (24) sets the flow rate of the back-washing water to be 0.4m according to a program3/m2·h~0.5m3/m2H, inputting a signal into a signal input end of the water outlet-backwashing shared water pump (17), controlling a frequency converter of the water outlet-backwashing shared water pump (17) to adjust the frequency, and ensuring that the flow of backwashing water is 0.4m3/m2·h~0.5m3/m2H, backwashing the ultrafiltration UF membrane component (11), discharging backwashing water into the membrane bioreactor (10), and when the liquid level in the membrane bioreactor (10) reaches the height of an overflow port, discharging the liquid into a sludge tank (27) through an overflow pipe (14), wherein the backwashing time is controlled to be 2-4 min;
fourthly, a sludge discharge stage: when sludge at the bottom of the membrane bioreactor (10) is accumulated to the bottom pipe wall of the aeration pipe (12), a sludge pump (25) is used for discharging the sludge to a sludge tank (27) through a sludge discharge valve (29) until the concentration of suspended solids at the bottom of the membrane bioreactor (10) is 20000 mg/L-25000 mg/L;
fifthly, a membrane cleaning stage: when the numerical value of the water outlet-back flush common pressure gauge (15) reaches 0.05MPa, closing all systems of the modified rice hull-ultrafiltration membrane bioreactor coupling device, taking out the ultrafiltration UF membrane component (11), and cleaning;
the modified rice hull-ultrafiltration membrane bioreactor coupling device consists of a water inlet system, a coagulation system, a membrane biological reaction system, a water outlet system, a back washing system, a sludge discharge system, a sludge backflow system and an automatic control system;
the water inlet system comprises a water inlet pool (1), a water inlet pump (2), a water inlet flow meter (3) and a water inlet control valve (4);
the coagulation system comprises a coagulation tank (5), a stirrer (6), a medicine inlet box (7), a coagulant adding pump (8) and a coagulant flow meter (31); a stirrer (6) is arranged in the coagulation tank (5);
the membrane biological reaction system comprises a filler adding box (9), a membrane bioreactor (10), an ultrafiltration UF membrane component (11), an aeration pipe (12), an aeration pump (13), an overflow pipe (14), a liquid level sensor (26) and a filler (30); the ultrafiltration UF membrane component (11) is arranged in the membrane bioreactor (10) in a hanging manner; the aeration pipe (12) is arranged below the ultrafiltration UF membrane module (11), and one end of the aeration pipe (12) is connected with an aeration pump (13);
the water outlet system comprises a water outlet-backwashing shared pressure gauge (15), a water outlet electromagnetic valve I (16), a water outlet-backwashing shared water pump (17), a water outlet electromagnetic valve II (18), a water outlet flow meter (19) and a water outlet pool (20);
the backwashing system comprises a backwashing electromagnetic valve I (21), a water outlet-backwashing shared water pump (17), a backwashing electromagnetic valve II (22), a water outlet-backwashing shared pressure gauge (15) and a backwashing flow meter (23);
the sludge discharge system comprises a sludge pump (25), a sludge discharge valve (29) and a sludge tank (27);
the sludge return system comprises a sludge pump (25) and a sludge return valve (28);
the automatic control system comprises a programmable logic controller (24), a liquid level sensor (26), a coagulant flow meter (31), a water outlet-backwashing shared pressure gauge (15), a water outlet electromagnetic valve I (16), a water outlet-backwashing shared water pump (17), a water outlet electromagnetic valve II (18), a water outlet flow meter (19), a backwashing electromagnetic valve I (21), a backwashing electromagnetic valve II (22), a backwashing flow meter (23) and a water inlet flow meter (3);
the coagulation tank (5) and the membrane bioreactor (10) are separated by an overflow wall, and the height of the overflow wall is lower than that of other side walls of the coagulation tank (5) and the membrane bioreactor (10);
the liquid level sensor (26) is arranged above the ultrafiltration UF membrane module (11) in a hanging mode, and the height of the tail end of a pointer of the liquid level sensor (26) is higher than the height of a water outlet of the ultrafiltration UF membrane module (11) and lower than the height of an overflow wall;
an overflow port is arranged on the side wall of the non-overflow wall of the membrane bioreactor (10), the height of the overflow port is lower than that of the overflow wall and higher than that of the tail end of a pointer of a liquid level sensor (26), the overflow port is communicated with one end of an overflow pipe (14), and the other end of the overflow pipe (14) is communicated with a sludge pool (27);
discharging sludge generated by the membrane biological reaction system through a sludge discharge system;
the sludge generated by the membrane biological reaction system flows back to enter the coagulation system through the sludge backflow system;
the automatic control system controls the on-off of the water outlet system and the back washing system;
and (3) normal water outlet stage: the backwashing electromagnetic valve I (21) and the backwashing electromagnetic valve II (22) are closed, the water outlet electromagnetic valve I (16) and the water outlet electromagnetic valve II (18) are opened, sewage to be treated enters the coagulation system through the water inlet system and then enters the membrane biological reaction system through overflow, and the treated sewage enters the water outlet system through the membrane biological reaction system.
2. The method for treating the low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, characterized in that the sewage to be treated is stored in a water inlet tank (1), and the sewage to be treated is sent into a coagulation tank (5) through a water inlet flow meter (3) and a water inlet control valve (4) by using a water inlet pump (2).
3. The method for treating the low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, which is characterized in that a coagulant is stored in a coagulant feeding tank (7), and the coagulant is fed into a coagulation tank (5) through a coagulant flow meter (31) by using a coagulant feeding pump (8).
4. The method for treating the low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice hull-ultrafiltration membrane bioreactor coupling device according to claim 1, wherein the filler (30) is stored in a filler adding box (9), and the filler (30) is added into the membrane bioreactor (10) through the filler adding box (9).
5. The method for treating the low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice hull-ultrafiltration membrane bioreactor coupling device according to claim 1, which is characterized in that a sludge outlet at the bottom of the membrane bioreactor (10) is communicated with a sludge tank (27) through a sludge pump (25) and a sludge discharge valve (29), and a sludge outlet at the bottom of the membrane bioreactor (10) is communicated with a coagulation tank (5) through the sludge pump (25) and a sludge return valve (28).
6. The method for treating the low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice hull-ultrafiltration membrane bioreactor coupling device according to claim 1, wherein the pH range of a polyvinylidene fluoride hollow fiber curtain membrane component in the ultrafiltration UF membrane component (11) is 2-10, the allowable operating pressure is 0.01-0.05 MPa, the membrane aperture is 0.02-0.2 μm, the outer diameter is 400-450 μm, the inner diameter is 320-350 μm, the membrane size is 80cm × 1000, the molecular weight cutoff 60000-100000 is realized, and the porosity is 40-50%.
7. The method for treating low-temperature low-turbidity high-color high-ammonia nitrogen source water by using the modified rice hull-ultrafiltration membrane bioreactor coupling device according to claim 1, wherein the activated sludge in the step one is obtained by the following steps: taking return sludge from a secondary sedimentation tank of a sewage plant, and obtaining activated sludge after acclimation and maturation.
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