CN106986448A - A kind of modified rice husk ultrafiltration membrane bioreactor coupling device and the method for handling low-temperature and low turbidity Gao Segao ammonia nitrogen source waters - Google Patents
A kind of modified rice husk ultrafiltration membrane bioreactor coupling device and the method for handling low-temperature and low turbidity Gao Segao ammonia nitrogen source waters Download PDFInfo
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- CN106986448A CN106986448A CN201710265878.1A CN201710265878A CN106986448A CN 106986448 A CN106986448 A CN 106986448A CN 201710265878 A CN201710265878 A CN 201710265878A CN 106986448 A CN106986448 A CN 106986448A
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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
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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
- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
A kind of modified rice husk ultrafiltration membrane bioreactor coupling device and the method for handling low-temperature and low turbidity Gao Segao ammonia nitrogen source waters, it is related to a kind of low-temperature and low turbidity Gao Segao ammonia nitrogen the water treatment devices and the method for handling low-temperature and low turbidity Gao Segao ammonia nitrogen source waters.The invention aims to solve existing processing low-temperature and low turbidity Gao Segao ammonia nitrogens water source water installations larger, the problem of the handling old high that there is installation area.The equipment is made up of water inlet system, coagulation system, membrane bio-reaction system, outlet system, backwashing system, sludge drainage system, sludge recirculation system and robot control system(RCS)；Method：First, startup stage；2nd, normal water outlet stage；3rd, the stage is backwashed；4th, the spoil disposal stage；5th, the Membrane cleaning stage.Advantage：Installation area is reduced, the cost of processed in units water is reduced.Present invention is mainly used for processing low-temperature and low turbidity Gao Segao ammonia nitrogen source waters.
Description
Technical field
The present invention relates to a kind of low-temperature and low turbidity Gao Segao ammonia nitrogen the water treatment devices and processing low-temperature and low turbidity Gao Segao ammonia
The method of nitrogen source water.
Background technology
In recent years, membrane technology is widely used to water treatment field, wherein, micro-filtration/ultrafiltration (MF/UF) film is used for running water
Production development is especially rapid.With the decline of film price, it be expected to substitution coagulation, precipitation sand filtration, sterilization etc. routinely drink it is aquatic
Production. art, as one of most important technological innovation of water treatment field.Membrane bioreactor (Membrane Bioreactor,
MBR) the incomparable advantage of active sludge, such as to suspended solid material, larger molecular organicses and microorganism in water
Have that good removal effect, technological process are short, floor space is few, sludge concentration is high, excess sludge production is few Deng, be easily achieved it is complete
Automatic operating management etc., but MBR is there is also deficiency, such as to microbial metabolic products, bacterium and dissolved organic matter (DOM)
It is very limited Deng removal ability, easily cause fouling membrane.Fouling membrane is the bottleneck for restricting UF-MBR technique popularization and application, its controlling party
Method is concentrated mainly in terms of improving into water pretreatment, membrane material exploitation, mud mixed liquid characteristic with optimization of operating condition 4, wherein
It is one of study hotspot of fouling membrane in recent years that mud mixed liquid characteristic, which improves, based on instant effect, the easily advantage, multidirectional MBR such as manipulation
The fillers such as middle addition suspension, particulate vector (activated carbon, zeolite, flyash, plastic grain) or flocculant alleviate fouling membrane, carry
The treatment effeciency of high system, but there is in terms of control membrane fouling problems with：1. suspension or particulate vector are circulated in MBR
In the presence of the potentiality on damage film surface during flowing；2. activity of the addition of coagulant easily to microbiologic population is negatively affected；
3. powder filler often uses Powdered Activated Carbon (PAC), but price is high, bio-regeneration is difficult etc. that drawback makes MBR by cost constraint
Limit its application.
Existing coagulation-membrane biological reaction technique is simply by coagulation and UF membrane simple combination, for coagulation and film biology
When reactor is respectively the split type combination of two separate units, installation area is larger, while the relatively big flocculating body of coagulation formation
It is broken by easily occurring during transmission pipeline, influence the performance of coagulation；Because of the mix stages and flocculated stage water of coagulating
Power condition imperfection and make that mixed flocculation effect is undesirable, dosage of PAC is larger, while because coagulation is insufficient, it is difficult to have
Imitating the fine flco or colloid concentration of coagulation gradually increases, and is easily caused fouling membrane, influence membrane flux and membrane lifetime, in the prior art
Also without the device of problems can be solved.
The content of the invention
The invention aims to solve existing processing low-temperature and low turbidity Gao Segao ammonia nitrogens water source water installations to have plant area
Area is larger, the problem of handling old high, and provides a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device and handle low
The method of the low turbid Gao Segao ammonia nitrogens source water of temperature.
A kind of modified rice husk-ultrafiltration membrane bioreactor coupling device, it is by water inlet system, coagulation system, membrane bioreaction
Answer system, outlet system, backwashing system, sludge drainage system, sludge recirculation system and robot control system(RCS) composition；
Described water inlet system includes intake pool, intake pump, feed water flow gauge and water inlet control valve door；
Described coagulation system includes coagulating basin, agitator, enters medicine-chest, coagulant dosage pump and coagulant flow gauge；
Agitator is set in coagulating basin；
Described membrane bio-reaction system including filler add case, membrane bioreactor, ultrafiltration UF membrane modules, aeration tube,
Aeration pump, overflow pipe, fluid level controller and filler；The ultrafiltration UF membrane modules are vacantly arranged in membrane bioreactor；It is described
Aeration tube is arranged on below ultrafiltration UF membrane modules, one end connection aeration pump of aeration tube；
Described outlet system includes water outlet-backwash and shares pressure gauge, water solenoid valve I, the shared water of water outlet-backwash
Pump, water solenoid valve II, water flow meter and discharge bay；
Described backwashing system include backwash magnetic valve I, water outlet-backwash share water pump, backwash magnetic valve II,
Water outlet-backwash shares pressure gauge and backwash flowmeter；
Described sludge drainage system includes sludge pump, spoil disposal valve and sludge-tank；
Described sludge recirculation system includes sludge pump and sludge reflux valve；
Described robot control system(RCS) includes programmable logic controller (PLC), fluid level controller, coagulant flow gauge, water outlet-recoil
Wash shared pressure gauge, water solenoid valve I, the shared water pump of water outlet-backwash, water solenoid valve II, water flow meter, backwash electricity
Magnet valve I, backwash magnetic valve II, backwash flowmeter and feed water flow gauge；
The coagulating basin is separated with membrane bioreactor by overflow wall, and overflow wall is highly biological less than coagulating basin and film
Other side walls of reactor；
The fluid level controller is vacantly arranged on above ultrafiltration UF membrane modules, and the pointer end height of fluid level controller is high
In ultrafiltration UF membrane module water outlet heights, less than overflow wall height；
Overfall is set on the side wall of membrane bioreactor non-overflow wall, and the height of overfall is high less than overflow wall
Degree, higher than the pointer end height of fluid level controller, overfall is connected with one end of overflow pipe, the other end and sludge of overflow pipe
Pond is connected；
The sludge produced by sludge drainage system to membrane bio-reaction system is discharged；
The sludge reflux that membrane bio-reaction system is produced is entered by coagulation system by sludge recirculation system；
Outlet system and backwashing system is controlled to switch by robot control system(RCS)；
The normal process stage：Backwash magnetic valve I and backwash magnetic valve II are closed, water solenoid valve I and water outlet electromagnetism
Valve II is opened, and treatment sewage enters coagulation system by water inlet system, then enters membrane bio-reaction system by overflow, processing
Sewage afterwards enters outlet system by membrane bio-reaction system；
The backwash stage：Water solenoid valve I and water solenoid valve II are closed, backwash magnetic valve I and backwash magnetic valve
II opens, and sewage sequentially passes through backwash magnetic valve I, water outlet-backwash and shares water pump, backwash after the processing of discharge bay storage
Magnetic valve II and backwash flowmeter, are backwashed by the delivery port of ultrafiltration UF membrane modules to ultrafiltration UF membrane modules.
One kind utilizes modified rice husk-ultrafiltration membrane bioreactor coupling device processing low-temperature and low turbidity Gao Segao ammonia nitrogen source waters
Method, be specifically realized by the following steps：
First, startup stage：Using low-temperature and low turbidity Gao Segao ammonia nitrogens source water as treatment sewage, treatment sewage is added
In membrane bioreactor, it is ensured that the liquid level for the treatment of sewage is less than the pointer end of liquid level sensor, and floods ultrafiltration UF completely
Membrane module, is then 15000mg/L~20000mg/L inoculation of activated-sludge by activated sludge concentration, and add case by filler
Filler is added in membrane bioreactor, it is ensured that in membrane bioreactor suspended sediment concentration be 20000mg/L~
25000mg/L, is started aeration pump, is aerated using continuous aeration mode, and liquid dissolved oxygen is dense in control membrane bioreactor
Spend for 6mg/L~7mg/L；Intake pump, coagulant dosage pump, agitator and programmable logic controller (PLC) are opened simultaneously, using entering
Treatment sewage from intake pool, feed water flow gauge and water inlet control valve door feeding is sequentially passed through by 28L/h of addition by water pump
In coagulating basin, coagulant is passed through into coagulant from medicine-chest is entered by 20mg/L~25mg/L of dosage using coagulant dosage pump
In flowmeter feeding coagulating basin, mixed using agitator under rotating speed 800r/min, sewage after coagulation in coagulating basin
When reaching overflow wall height, the sewage after coagulation is by overflow wall from coagulating basin overflow enters membrane bioreactor；When film is biological
When liquid contacts the pointer of liquid level sensor in reactor, this signal inputs programmable logic controller (PLC) by liquid level sensor, this
When PLC controls water solenoid valve I, water outlet-backwash shares water pump and water solenoid valve II is opened, utilize
Programmable logic controller (PLC) records treatment sewage addition and coagulant respectively according to feed water flow gauge and coagulant flow gauge
Addition, opens sludge reflux valve while water outlet-backwash shares starting mode of pump, and starts sludge pump, carries out sludge
Backflow, is 500mg/L~900mg/L by sludge concentration value control in coagulating basin, startup stage terminates；
2nd, normal water outlet stage：Using intake pump continue by treatment sewage from intake pool, by 28L/h of addition according to
In secondary process feed water flow gauge and water inlet control valve door feeding coagulating basin, coagulant is continued from entering medicine using coagulant dosage pump
Case, by 10mg/L~15mg/L of dosage by coagulant flow gauge feeding coagulating basin, controlling the rotating speed 800r/ of agitator
Min, hydraulic detention time is 2min in coagulating basin；And using programmable logic controller (PLC) according to feed water flow gauge and coagulant
Flowmeter records treatment sewage addition and coagulant addition respectively, and aeration pump is persistently aerated using continuous aeration mode,
It is 6mg/L~7mg/L to control liquid dissolved oxygen concentration in membrane bioreactor；In order to ensure suspended solid in membrane bioreactor
Concentration is 20000mg/L~25000mg/L, in time the modified rice husk of supplement, the water outlet that sewage passes through ultrafiltration UF membrane modules after processing
Mouthful, sequentially pass through water solenoid valve I, water outlet-backwash shared water pump, water solenoid valve II and water flow meter and enter discharge bay
In；By numeric feedback to programmable logic controller (PLC) during water flow timing, by programmable logic controller (PLC) adjusting water outlet-anti-
Rinse and share water pump frequency, it is ensured that using water yield as 130L/m2H~160L/m2H water outlets；The waterpower in membrane bioreactor
Residence time is 2h；
3rd, the stage is backwashed：According to water flow meter feedback information, 25min~30min is reached when the continuous effluent time
When, PLC controls water solenoid valve I and water solenoid valve II are closed, while controlling the backwash He of magnetic valve I
Backwash magnetic valve II is opened, and to sequentially pass through backwash magnetic valve I, water outlet-backwash common for sewage after the processing of discharge bay storage
With water pump, backwash magnetic valve II and backwash flowmeter, ultrafiltration UF membrane modules are entered by the delivery port of ultrafiltration UF membrane modules
Row backwash；It is 0.4m that programmable logic controller (PLC) backwashes water flow according to program setting3/m2H~0.5m3/m2H,
And the signal input part that water outlet-backwash shares water pump is input a signal into, control water outlet-backwash shares the regulation of pump variable frequency device
Frequency, it is ensured that to backwash water flow as 0.4m3/m2H~0.5m3/m2H is backwashed to ultrafiltration UF membrane modules, instead
Flushing water is drained into membrane bioreactor, when liquid level reaches overflow open height in membrane bioreactor, is drained into by overflow pipe
In sludge-tank, backwashing time is controlled in 2min~4min；
4th, the spoil disposal stage：When membrane bioreactor base sludge builds up to aeration tube bottom tube wall, using sludge pump through row
Slurry valve goalkeeper's sludge drains into sludge-tank, is 20000mg/L~25000mg/L to membrane bioreactor bottom suspended sediment concentration；
5th, the Membrane cleaning stage：When water outlet-backwash, which shares pressure gauge numerical value, reaches 0.05MPa, the modified rice husk of closing-super
All systems of membrane filter bioreactor coupling device, take out ultrafiltration UF membrane modules, are cleaned.
Advantage of the present invention：
1st, coagulating basin and membrane bioreactor unitary design, water pump is shared using water outlet-backwash, reduces plant area
Area.
2nd, front end sets coagulating basin, and dosing coagulant is to remove larger molecular organicses.Avoid because macromolecular is organic in water
Thing etc. is attached to film surface, the problem of backwash workload is big.
3rd, add high concentration be modified rice hull active carbon, formed cake layer, reduce fouling membrane, prolonging service lifetime of film, and then
Reduce the cost of processed in units water.
4th, sludge recirculation system is provided with, coagulation agent content is reduced using sludge reflux, is slowed down to biological suppression；Avoid
Excessive coagulant causes Biostatic into membrane bioreactor and reduces removal effect of the activated sludge to ammonia nitrogen.
Water outlet-backwash shares water pump and continuously run when the 5th, sharing water pump, water outlet and recoil, reduces normally on and normally off to water pump
Loss.
6th, ammonia nitrogen removal cycle, activated sludge replacing construction and reasonable disposition be can determine that.
Brief description of the drawings
Fig. 1 is modified rice husk of the present invention-ultrafiltration membrane bioreactor coupling mechanism structure schematic diagram.
Embodiment
Embodiment one：With reference to Fig. 1, present embodiment is a kind of modified rice husk-ultrafiltration membrane bioreactor coupling
Device, it is returned by water inlet system, coagulation system, membrane bio-reaction system, outlet system, backwashing system, sludge drainage system, sludge
Streaming system and robot control system(RCS) composition；
Described water inlet system includes intake pool 1, intake pump 2, feed water flow gauge 3 and water inlet control valve door 4；
Described coagulation system includes coagulating basin 5, agitator 6, enters medicine-chest 7, coagulant dosage pump 8 and coagulant flow gauge
31；Agitator 6 is set in coagulating basin 5；
Described membrane bio-reaction system adds case 9, membrane bioreactor 10, ultrafiltration UF membrane modules 11, exposure including filler
Tracheae 12, aeration pump 13, overflow pipe 14, fluid level controller 26 and filler 30；The ultrafiltration UF membrane modules 11 are vacantly arranged on film
In bioreactor 10；The aeration tube 12 is arranged on the lower section of ultrafiltration UF membrane modules 11, one end connection aeration pump of aeration tube 12
13；
Described outlet system is common including the shared pressure gauge 15 of water outlet-backwash, water solenoid valve I 16, water outlet-backwash
With water pump 17, water solenoid valve II 18, water flow meter 19 and discharge bay 20；
Described backwashing system includes backwash magnetic valve I 21, water outlet-backwash and shares water pump 17, backwash electromagnetism
Valve II 22, water outlet-backwash share pressure gauge 15 and backwash flowmeter 23；
Described sludge drainage system includes sludge pump 25, spoil disposal valve 29 and sludge-tank 27；
Described sludge recirculation system includes sludge pump 25 and sludge reflux valve 28；
Described robot control system(RCS) includes programmable logic controller (PLC) 24, fluid level controller 26, coagulant flow gauge 31, gone out
Water-backwash shares pressure gauge 15, water solenoid valve I 16, water outlet-backwash shared water pump 17, water solenoid valve II 18, water outlet
Flowmeter 19, backwash magnetic valve I 21, backwash magnetic valve II 22, backwash flowmeter 23 and feed water flow gauge 3；
The coagulating basin 5 is separated with membrane bioreactor 10 by overflow wall, and overflow wall is highly less than coagulating basin 5 and film
Other side walls of bioreactor 10；
The fluid level controller 26 is vacantly arranged on the top of ultrafiltration UF membrane modules 11, and the pointer end of fluid level controller 26
Highly it is higher than the water outlet height of ultrafiltration UF membrane modules 11, less than overflow wall height；
Overfall is set on the side wall of the non-overflow wall of membrane bioreactor 10, and the height of overfall is high less than overflow wall
Degree, higher than the pointer end height of fluid level controller 26, overfall is connected with one end of overflow pipe 14, the other end of overflow pipe 14
Connected with sludge-tank 27；
The sludge produced by sludge drainage system to membrane bio-reaction system is discharged；
The sludge reflux that membrane bio-reaction system is produced is entered by coagulation system by sludge recirculation system；
Outlet system and backwashing system is controlled to switch by robot control system(RCS)；
The normal process stage：Backwash magnetic valve I 21 and backwash magnetic valve II 22 is closed, water solenoid valve I 16 and go out
Water solenoid valve II 18 is opened, and treatment sewage enters coagulation system by water inlet system, then enters membrane biological reaction by overflow
System, the sewage after processing enters outlet system by membrane bio-reaction system；
The backwash stage：Water solenoid valve I 16 and water solenoid valve II 18 are closed, backwash magnetic valve I 21 and backwash
Magnetic valve II 22 is opened, and to sequentially pass through backwash magnetic valve I 21, water outlet-backwash common for sewage after the processing that discharge bay 20 is deposited
With water pump 17, backwash magnetic valve II 22 and backwash flowmeter 23, by the delivery port of ultrafiltration UF membrane modules 11 to ultrafiltration UF
Membrane module 11 is backwashed.
Sewage in coagulating basin 5 described in present embodiment after coagulation enters film from the overflow of coagulating basin 5 by overflow wall and given birth to
In thing reactor 10.
Present embodiment is when liquid contacts the pointer of liquid level sensor 26 in membrane bioreactor 10, and this signal is by liquid level
Sensor 26 input programmable logic controller (PLC) 24, now programmable logic controller (PLC) 24 control water solenoid valve I 16, water outlet-
Backwash shares water pump 17 and water solenoid valve II 18 is opened.
Ultrafiltration UF membrane modules 11 described in present embodiment are middle Kynoar hollow fiber curtain type film assembly, by Tianjin film
Its Science and Technology Co., Ltd. produces, and its pH scope is 2~10；Permission operating pressure is 0.01MPa~0.05MPa；Membrane aperture
0.02 μm~0.2 μm；400 μm~450 μm of external diameter, 320 μm~350 μm of internal diameter；Film size 80cm × 1000 piece；It retains molecule
Measure as 60000~100000；Porosity is 40%~50%.
Fig. 1 is 1 table in modified rice husk of the present invention-ultrafiltration membrane bioreactor coupling mechanism structure schematic diagram, figure
Show intake pool；2 represent intake pump；3 represent feed water flow gauge；4 represent water inlet control valve door；5 represent coagulating basin；6 represent stirring
Device；7 represent into medicine-chest；8 represent coagulant dosage pump；9 expression fillers add case；10 represent membrane bioreactor；11 represent super
Filter UF membrane modules；12 represent aeration tube；13 represent aeration pump；14 represent overflow pipe；15 represent that water outlet-backwash shares pressure
Table；16 represent water solenoid valve I；17 represent that water outlet-backwash shares water pump；18 represent water solenoid valve II；19 represent water outlet
Flowmeter；20 represent discharge bay；21 represent backwash magnetic valve I；22 represent backwash magnetic valve II；23 represent backwash flow
Meter；24 represent programmable logic controller (PLC)；25 represent sludge pump；26 represent fluid level controller；27 represent sludge-tank；28 represent dirty
Mud return valve；29 represent spoil disposal valve；30 represent filler；31 represent coagulant flow gauge.
The present invention attempts high concentration modification rice husk being added in UF-MBR, forms modified rice husk-UF-MBR group technologies,
UF-MBR, the modified parallel systems of rice husk-UF-MBR two are studied in the scavenging effects of low temperature Gao Segao ammonia nitrogen source waters, reactor
Activated sludge performance and fouling membrane situation, investigate the mechanism of action and efficiency of modified rice husk, explore processing low temperature Gao Segao ammonia
Nitrogen source water or the new method for effectively slowing down MBR fouling membranes, and provide technology branch for the popularization and application for being modified rice husk-UF-MBR
Hold.
Amorphous hydrated silica content is 15%~20% in rice husk, and other main components are hydrocarbon.Rice
Shell has the features such as silicone content is big, porous capacity is small, quality is coarse, and the activated carbon of production has by force to a variety of organic compounds
Adsorption capacity, and objectionable impurities (such as lead, arsenic) is not contained, available for a variety of industries such as water process, with huge market potential,
The activated carbon product cost that rice husk raw material is sufficient, cheap, thus produce is low, had not only saved the energy but also had realized waste resource
Change, meet sustainable development requirement, with larger practical value and application prospect.
The feasibility that Proof-Of Principle is modified rice husk-UF-MBR group technologies is slowed down based on fouling membrane：Modified rice husk-UF-MBR
Group technology integrates the strong suction-operated for being modified rice husk, MBR biodegradation and the efficient crown_interception of film, its semilate rice
There is based active carbon huge specific surface area and flourishing pore structure to be easy to adsorption and enrichment organic matter, while being also microorganism
The good carrier of apposition growth so that the bioactivity of whole system is high, stability is strong；Modified rice husk absorbed portion microorganism
Extracellular polymeric, film surface formed cake layer, can effectively decelerating membrane pollution and cross mould poor (TMP) growth rate,
There is protective effect to membrane module.Therefore it is modified adding there is a possibility that the performance of activated sludge is changed in reactor for rice husk
It is kind, increase film water flux, effective decelerating membrane pollution, making the effluent quality of UF-MBR systems is improved, and pollutant is gone
Except efficiency is more reliable and more stable, the ability of system attack impact load is improved.
Precipitating sludge in membrane bioreactor 10 is back to coagulating basin 5, can improve the coagulation effect of low-cloudy water；In addition,
Adsorb a large amount of ammonia nitrogens, the modification rice husk of organic matter can be the green new and high technology of current environment using renewable resource as fertilizer
Development trend；The 65000000 tons of stalks and 80,000,000 tons of animal dungs that Heilongjiang Province rural is produced every year (cause Gao Segao ammonia nitrogens
Water quality major reason) need to be effectively addressed.
Embodiment two：With reference to Fig. 1, the difference of present embodiment and embodiment one is：Pending dirt
Water is stored in intake pool 1, using intake pump 2 that treatment sewage is mixed by feed water flow gauge 3 and the feeding of water inlet control valve door 4
In solidifying pond 5.Other are identical with embodiment one.
Embodiment three：With reference to Fig. 1, one of present embodiment and embodiment one or two difference are：It is mixed
Solidifying agent is stored in into medicine-chest 7, is sent into coagulant in coagulating basin 5 by coagulant flow gauge 31 using coagulant dosage pump 8.
Other are identical with embodiment one or two.
Embodiment four：With reference to Fig. 1, one of present embodiment and embodiment one to three difference are：Fill out
Material 30 is stored in filler and added in case 9, and adding case 9 by filler is added to filler 30 in membrane bioreactor 10.Other with
Embodiment one to three is identical.
Embodiment five：With reference to Fig. 1, one of present embodiment and embodiment one to four difference are：
The bottom mud mouth of membrane bioreactor 10 is connected by sludge pump 25 and spoil disposal valve 29 with sludge-tank 27, in membrane bioreactor
10 bottom mud mouths are connected by sludge pump 25 and sludge reflux valve 28 with coagulating basin 5.Other with embodiment one to
Four is identical.
Embodiment six：With reference to Fig. 1, one of present embodiment and embodiment one to five difference are：Institute
The ultrafiltration UF membrane modules 11 stated are middle Kynoar hollow fiber curtain type film assembly, and pH scopes are 2~10；Allow operating pressure be
0.01MPa~0.05MPa；0.02 μm~0.2 μm of membrane aperture；400 μm~450 μm of external diameter, 320 μm~350 μm of internal diameter；Film size
80cm × 1000 piece；Its molecular cut off is 60000~100000；Porosity is 40%~50%.Other and specific embodiment party
Formula one to five is identical.
Embodiment seven：With reference to Fig. 1, present embodiment is that a kind of utilize is modified rice husk-ultrafiltration membrane bioreactor
The method that coupling device handles low-temperature and low turbidity Gao Segao ammonia nitrogen source waters, it is characterised in that it is completed according to the following steps：
First, startup stage：Using low-temperature and low turbidity Gao Segao ammonia nitrogens source water as treatment sewage, treatment sewage is added
In membrane bioreactor 10, it is ensured that the liquid level for the treatment of sewage is less than the pointer end of liquid level sensor 26, and floods completely super
UF membrane modules 11 are filtered, are then 15000mg/L~20000mg/L inoculation of activated-sludge by activated sludge concentration, and pass through filler
Add case 9 filler 30 is added in membrane bioreactor 10, it is ensured that suspended sediment concentration is in membrane bioreactor 10
20000mg/L~25000mg/L, is started aeration pump 13, is aerated using continuous aeration mode, controls membrane bioreactor 10
Middle liquid dissolved oxygen concentration is 6mg/L~7mg/L；Intake pump 2, coagulant dosage pump 8, agitator 6 are opened simultaneously and may be programmed
Logic controller 24, flow of inlet water is sequentially passed through using intake pump 2 from intake pool 1 by treatment sewage by 28L/h of addition
Meter 3 and water inlet control valve door 4 are sent into coagulating basin 5, using coagulant dosage pump 8 by coagulant from entering medicine-chest 7, using dosage as
20mg/L~25mg/L using agitator 6 under rotating speed 800r/min by the feeding coagulating basin 5 of coagulant flow gauge 31, being carried out
Mix, when the sewage after coagulation in coagulating basin 5 reaches overflow wall height, sewage after coagulation is by overflow wall from coagulating basin 5
Overflow enters in membrane bioreactor 10；When liquid contacts the pointer of liquid level sensor 26 in membrane bioreactor 10, this signal
Programmable logic controller (PLC) 24 is inputted by liquid level sensor 26, the now control of programmable logic controller (PLC) 24 water solenoid valve I 16,
Water outlet-backwash shares water pump 17 and water solenoid valve II 18 is opened, using programmable logic controller (PLC) 24 according to flow of inlet water
Meter 3 and coagulant flow gauge 31 record treatment sewage addition and coagulant addition respectively, and water is shared in water outlet-backwash
Sludge reflux valve 28 is opened while pump 17 starts, and starts sludge pump 25, sludge reflux is carried out, by sludge in coagulating basin 5
Concentration value control is 500mg/L~900mg/L, and startup stage terminates；
2nd, normal water outlet stage：Continued using intake pump 2 by treatment sewage from intake pool 1, using addition as 28L/h
Sequentially pass through feed water flow gauge 3 and water inlet control valve door 4 is sent into coagulating basin 5, continued using coagulant dosage pump 8 from entering medicine-chest
7 into coagulating basin 5 dosing coagulant, by 10mg/L~15mg/L of dosage by coagulant flow gauge 31 send into coagulating basin 5
In, the rotating speed 800r/min of agitator 6 is controlled, hydraulic detention time is 2min in coagulating basin 5；And utilize FPGA control
Device 24 processed records treatment sewage addition and coagulant addition respectively according to feed water flow gauge 3 and coagulant flow gauge 31,
Aeration pump 13 is persistently aerated using continuous aeration mode, control in membrane bioreactor 10 liquid dissolved oxygen concentration for 6mg/L~
7mg/L；In order to ensure that suspended sediment concentration is 20000mg/L~25000mg/L, timely additional fillers in membrane bioreactor 10
30, sewage is sequentially passed through water solenoid valve I 16, water outlet-backwash and shared by the delivery port of ultrafiltration UF membrane modules 11 after processing
Water pump 17, water solenoid valve II 18 and water flow meter 19 enter in discharge bay 20；Water flow meter 19 is constantly by numeric feedback
To programmable logic controller (PLC) 24, the frequency of water pump 17 is shared by 24 adjusting water outlets of programmable logic controller (PLC)-backwash, it is ensured that
Using water yield as 130L/m2H~160L/m2H water outlets；Hydraulic detention time is 2h in membrane bioreactor 10；
3rd, the stage is backwashed：According to the feedback information of water flow meter 19,25min~30min is reached when the continuous effluent time
When, the control water solenoid valve I 16 of programmable logic controller (PLC) 24 and water solenoid valve II 18 are closed, while controlling backwash electromagnetism
Valve I 21 and backwash magnetic valve II 22 open, discharge bay 20 deposit processing after sewage sequentially pass through backwash magnetic valve I 21,
Water outlet-backwash shares water pump 17, backwash magnetic valve II 22 and backwash flowmeter 23, passes through going out for ultrafiltration UF membrane modules 11
The mouth of a river is backwashed to ultrafiltration UF membrane modules 11；Programmable logic controller (PLC) 24 backwashes water flow according to program setting
0.4m3/m2H~0.5m3/m2H, and the signal input part that water outlet-backwash shares water pump 17 is input a signal into, control out
Water-backwash shares the frequency converter regulating frequency of water pump 17, it is ensured that to backwash water flow as 0.4m3/m2H~0.5m3/
m2H is backwashed to ultrafiltration UF membrane modules 11, and backwashing water is drained into membrane bioreactor 10, when membrane bioreactor 10
When interior liquid level reaches overflow open height, drained into by overflow pipe 14 in sludge-tank 27, backwashing time is controlled in 2min~4min；
4th, the spoil disposal stage：When the base sludge of membrane bioreactor 10 builds up to 12 bottom tube wall of aeration tube, sludge pump is utilized
Sludge is drained into sludge-tank 27 by 25 through spoil disposal valve 29, is 20000mg/L to the bottom suspended sediment concentration of membrane bioreactor 10
~25000mg/L；
5th, the Membrane cleaning stage：When water outlet-backwash, which shares the numerical value of pressure gauge 15, reaches 0.05MPa, the modified rice husk of closing-
All systems of ultrafiltration membrane bioreactor coupling device, take out ultrafiltration UF membrane modules 11, are cleaned.
Embodiment eight：The difference of present embodiment and embodiment seven is：Periodically to film in step 2
Organic carbon source is added in bioreactor 10, it is ensured that the COD of liquid in membrane bioreactor 10Mn5mg/L~7mg/L, TOC6mg/
L~8mg/L, pH=7.Other are identical with embodiment seven.
Embodiment nine：One of present embodiment and embodiment seven or eight difference is：Institute in step one
It is modified rice hull active carbon to state filler 30.Other are identical with embodiment seven or eight.
Embodiment ten：The difference of present embodiment and embodiment nine is：The modified rice husk activity
Charcoal is obtained according to the following steps：4h is soaked through 1mol/LHCl solution after rice husk removal of impurities, washing, it is 7~8 to be washed to pH value,
Temperature is dry at 100 DEG C, removes K+、Na+、Ca2+、Fe2+、Mg2+, dried rice husk insert Muffle furnace isolation 800 DEG C of air
Be carbonized 3h, and 0.2g carbonization rice husks and 20mL 1.5mol/LNaOH solution are heated to reflux into 2h, is filtered, and is obtained filter residue and is washed to
PH value is 7~8, and it is modified rice hull active carbon head product to dry, and modified rice hull active carbon is made through 600 DEG C of high-temperature activations.Its
He is identical with embodiment nine.
Embodiment 11：One of present embodiment and embodiment seven to ten difference is：In step one
The activated sludge is obtained according to the following steps：The returned sludge of sewage plant secondary sedimentation tank is derived from, after domestication maturation, i.e.,
Obtain activated sludge.Other are identical with embodiment seven to ten.
Using following verification experimental verifications effect of the present invention
Embodiment 1：With reference to Fig. 1, a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device, it is by water inlet system, mixed
Solidifying system, membrane bio-reaction system, outlet system, backwashing system, sludge drainage system, sludge recirculation system and robot control system(RCS) group
Into；
Described water inlet system includes intake pool 1, intake pump 2, feed water flow gauge 3 and water inlet control valve door 4；
Described coagulation system includes coagulating basin 5, agitator 6, enters medicine-chest 7, coagulant dosage pump 8 and coagulant flow gauge
31；Agitator 6 is set in coagulating basin 5；
Described membrane bio-reaction system adds case 9, membrane bioreactor 10, ultrafiltration UF membrane modules 11, exposure including filler
Tracheae 12, aeration pump 13, overflow pipe 14, fluid level controller 26 and filler 30；The ultrafiltration UF membrane modules 11 are vacantly arranged on film
In bioreactor 10；The aeration tube 12 is arranged on the lower section of ultrafiltration UF membrane modules 11, one end connection aeration pump of aeration tube 12
13；
Described outlet system is common including the shared pressure gauge 15 of water outlet-backwash, water solenoid valve I 16, water outlet-backwash
With water pump 17, water solenoid valve II 18, water flow meter 19 and discharge bay 20；
Described backwashing system includes backwash magnetic valve I 21, water outlet-backwash and shares water pump 17, backwash electromagnetism
Valve II 22, water outlet-backwash share pressure gauge 15 and backwash flowmeter 23；
Described sludge drainage system includes sludge pump 25, spoil disposal valve 29 and sludge-tank 27；
Described sludge recirculation system includes sludge pump 25 and sludge reflux valve 28；
Described robot control system(RCS) includes programmable logic controller (PLC) 24, fluid level controller 26, coagulant flow gauge 31, gone out
Water-backwash shares pressure gauge 15, water solenoid valve I 16, water outlet-backwash shared water pump 17, water solenoid valve II 18, water outlet
Flowmeter 19, backwash magnetic valve I 21, backwash magnetic valve II 22, backwash flowmeter 23 and feed water flow gauge 3；
The coagulating basin 5 is separated with membrane bioreactor 10 by overflow wall, and overflow wall is highly less than coagulating basin 5 and film
Other side walls of bioreactor 10；
The fluid level controller 26 is vacantly arranged on the top of ultrafiltration UF membrane modules 11, and the pointer end of fluid level controller 26
Highly it is higher than the water outlet height of ultrafiltration UF membrane modules 11, less than overflow wall height；
Overfall is set on the side wall of the non-overflow wall of membrane bioreactor 10, and the height of overfall is high less than overflow wall
Degree, higher than the pointer end height of fluid level controller 26, overfall is connected with one end of overflow pipe 14, the other end of overflow pipe 14
Connected with sludge-tank 27；
The sludge produced by sludge drainage system to membrane bio-reaction system is discharged；Film is given birth to by sludge recirculation system
The sludge reflux that thing reaction system is produced enters coagulation system；Outlet system and backwashing system is controlled to open by robot control system(RCS)
Close；
Coagulant is stored in into medicine-chest 7, is sent into coagulant by coagulant flow gauge 31 using coagulant dosage pump 8
In coagulating basin 5.
Filler 30 is stored in filler and added in case 9, and adding case 9 by filler 30 by filler is added to membrane bioreactor 10
In.
When liquid contacts the pointer of liquid level sensor 26 in membrane bioreactor 10, this signal is defeated by liquid level sensor 26
Enter programmable logic controller (PLC) 24, the now control of programmable logic controller (PLC) 24 water solenoid valve I 16, water outlet-backwash are shared
Water pump 17 and water solenoid valve II 18 are opened.
Connected in the bottom mud mouth of membrane bioreactor 10 by sludge pump 25 and spoil disposal valve 29 with sludge-tank 27, in film
The bottom mud mouth of bioreactor 10 is connected by sludge pump 25 and sludge reflux valve 28 with coagulating basin 5.
Sewage sequentially passes through water solenoid valve I 16, water outlet-recoil by the delivery port of ultrafiltration UF membrane modules 11 after processing
Shared water pump 17, water solenoid valve II 18 and water flow meter 19 is washed to enter in discharge bay 20.
Described ultrafiltration UF membrane modules 11 are middle Kynoar hollow fiber curtain type film assembly, and pH scopes are 2~10；Allow
Operating pressure is 0.01MPa~0.05MPa；0.02 μm~0.2 μm of membrane aperture；400 μm~450 μm of external diameter, 320 μm of internal diameter~
350μm；Film size 80cm × 1000 piece；Its molecular cut off is 60000~100000；Porosity is 40%~50%.
The normal process stage：Backwash magnetic valve I 21 and backwash magnetic valve II 22 is closed, water solenoid valve I 16 and go out
Water solenoid valve II 18 is opened, and treatment sewage is stored in intake pool 1, and treatment sewage is passed through into feed water flow using intake pump 2
Gauge 3 and water inlet control valve door 4 are sent into coagulating basin 5；Sewage in coagulating basin 5 after coagulation is by overflow wall from coagulating basin
5 overflows enter in membrane bioreactor 10；Sewage sequentially passes through water outlet electromagnetism by the delivery port of ultrafiltration UF membrane modules 11 after processing
Valve I 16, water outlet-backwash share water pump 17, water solenoid valve II 18 and water flow meter 19 and entered in discharge bay 20.
The backwash stage：Water solenoid valve I 16 and water solenoid valve II 18 are closed, backwash magnetic valve I 21 and backwash
Magnetic valve II 22 is opened, and to sequentially pass through backwash magnetic valve I 21, water outlet-backwash common for sewage after the processing that discharge bay 20 is deposited
With water pump 17, backwash magnetic valve II 22 and backwash flowmeter 23, by the delivery port of ultrafiltration UF membrane modules 11 to ultrafiltration UF
Membrane module 11 is backwashed.
Embodiment 2：With reference to Fig. 1, one kind utilizes modified rice husk-ultrafiltration membrane bioreactor coupling device processing low-temperature and low turbidity
The method of Gao Segao ammonia nitrogen source waters, is specifically realized by the following steps：
First, startup stage：Using low-temperature and low turbidity Gao Segao ammonia nitrogens source water as treatment sewage, treatment sewage is added
In membrane bioreactor 10, it is ensured that the liquid level for the treatment of sewage is less than the pointer end of liquid level sensor 26, and floods completely super
UF membrane modules 11 are filtered, are then 15000mg/L~20000mg/L inoculation of activated-sludge by activated sludge concentration, and pass through filler
Add case 9 filler 30 is added in membrane bioreactor 10, it is ensured that suspended sediment concentration is in membrane bioreactor 10
20000mg/L~25000mg/L, is started aeration pump 13, is aerated using continuous aeration mode, controls membrane bioreactor 10
Middle liquid dissolved oxygen concentration is 6mg/L~7mg/L；Intake pump 2, coagulant dosage pump 8, agitator 6 are opened simultaneously and may be programmed
Logic controller 24, flow of inlet water is sequentially passed through using intake pump 2 from intake pool 1 by treatment sewage by 28L/h of addition
Meter 3 and water inlet control valve door 4 are sent into coagulating basin 5, continue to add into coagulating basin 5 from entering medicine-chest 7 using coagulant dosage pump 8
Coagulant, by 20mg/L~25mg/L of dosage by the feeding coagulating basin 5 of coagulant flow gauge 31, being existed using agitator 6
Mixed under rotating speed 800r/min, when the sewage after coagulation in coagulating basin 5 reaches overflow wall height, the sewage after coagulation leads to
Cross overflow wall from the overflow of coagulating basin 5 to enter in membrane bioreactor 10, small wadding grain is contained in the sewage after the coagulation；When film life
When liquid contacts the pointer of liquid level sensor 26 in thing reactor 10, this signal inputs FPGA control by liquid level sensor 26
Device 24 processed, the now control of programmable logic controller (PLC) 24 water solenoid valve I 16, water outlet-backwash share water pump 17 and go out water power
Magnet valve II 18 is opened, and is recorded and treated respectively according to feed water flow gauge 3 and coagulant flow gauge 31 using programmable logic controller (PLC) 24
Sewage addition and coagulant addition are handled, is shared in water outlet-backwash while water pump 17 starts and opens sludge reflux valve
Door 28, and start sludge pump 25, sludge reflux is carried out, is 500mg/L~900mg/L by sludge concentration value control in coagulating basin 5,
Startup stage terminates；
2nd, normal water outlet stage：Continued using intake pump 2 by treatment sewage from intake pool 1, using addition as 28L/h
Sequentially pass through feed water flow gauge 3 and water inlet control valve door 4 send into coagulating basin 5 in, using coagulant dosage pump 8 continue coagulant from
Enter medicine-chest 7, by 10mg/L~15mg/L of dosage by the feeding coagulating basin 5 of coagulant flow gauge 31, controlling agitator 6
Rotating speed 800r/min, hydraulic detention time is 2min in coagulating basin 5；And using programmable logic controller (PLC) 24 according to feed water flow
Gauge 3 and coagulant flow gauge 31 record treatment sewage addition and coagulant addition respectively, and aeration pump 13 is using continuous
Aeration mode is persistently aerated, and it is 6mg/L~7mg/L to control liquid dissolved oxygen concentration in membrane bioreactor 10；The disturbance of bubble
Membrane biological reaction area is formed small vortex, prevent flco from sinking, mutual collision and flocculation beneficial to flco, and then realize
Abundant absorption to pollutant, is aerated the abundant dissolved oxygen provided, is conducive to the growth and breeding of microorganism, carries out biodegradable
To improve the effect of water process；In order to ensure that suspended sediment concentration is 20000mg/L~25000mg/ in membrane bioreactor 10
L, timely additional fillers 30, after processing sewage by the delivery ports of ultrafiltration UF membrane modules 11, sequentially pass through water solenoid valve I 16,
Water outlet-backwash shares water pump 17, water solenoid valve II 18 and water flow meter 19 and entered in discharge bay 20；Water flow meter 19
Constantly numeric feedback is shared to programmable logic controller (PLC) 24 by 24 adjusting water outlets of programmable logic controller (PLC)-backwash
The frequency of water pump 17, it is ensured that using water yield as 130L/m2H~160L/m2H water outlets；The hydraulic retention in membrane bioreactor 10
Time is 2h；
3rd, the stage is backwashed：According to the feedback information of water flow meter 19,25min~30min is reached when the continuous effluent time
When, the control water solenoid valve I 16 of programmable logic controller (PLC) 24 and water solenoid valve II 18 are closed, while controlling backwash electromagnetism
Valve I 21 and backwash magnetic valve II 22 open, discharge bay 20 deposit processing after sewage sequentially pass through backwash magnetic valve I 21,
Water outlet-backwash shares water pump 17, backwash magnetic valve II 22 and backwash flowmeter 23, passes through going out for ultrafiltration UF membrane modules 11
The mouth of a river is backwashed to ultrafiltration UF membrane modules 11；Programmable logic controller (PLC) 24 backwashes water flow according to program setting
0.4m3/m2H~0.5m3/m2H, and the signal input part that water outlet-backwash shares water pump 17 is input a signal into, control out
Water-backwash shares the frequency converter regulating frequency of water pump 17, it is ensured that to backwash water flow as 0.4m3/m2H~0.5m3/
m2H is backwashed to ultrafiltration UF membrane modules 11, and backwashing water is drained into membrane bioreactor 10, when membrane bioreactor 10
When interior liquid level reaches overflow open height, drained into by overflow pipe 14 in sludge-tank 27, backwashing time is controlled in 2min~4min；
4th, the spoil disposal stage：When the base sludge of membrane bioreactor 10 builds up to 12 bottom tube wall of aeration tube, sludge pump is utilized
Sludge is drained into sludge-tank 27 by 25 through spoil disposal valve 29, is 20000mg/L to the bottom suspended sediment concentration of membrane bioreactor 10
~25000mg/L；
5th, the Membrane cleaning stage：When water outlet-backwash, which shares the numerical value of pressure gauge 15, reaches 0.05MPa, the modified rice husk of closing-
All systems of ultrafiltration membrane bioreactor coupling device, take out ultrafiltration UF membrane modules 11, are cleaned.
Periodically organic carbon source is added in the present embodiment step 2 into membrane bioreactor 10, it is ensured that membrane bioreactor 10
The COD of middle liquidMn5mg/L~7mg/L, TOC 6mg/L~8mg/L, pH=7.
Filler 30 described in the present embodiment step one is modified rice hull active carbon；The modified rice hull active carbon is by following
What step was obtained：4h is soaked through 1mol/L HCl solutions after rice husk removal of impurities, washing, it is 7~8 to be washed to pH value, be 100 in temperature
Dried at DEG C, remove K+、Na+、Ca2+、Fe2+、Mg2+, dried rice husk inserts Muffle furnace isolation 800 DEG C of air carbonization 3h, will
0.2g carbonization rice husks and 20mL 1.5mol/LNaOH solution are heated to reflux 2h, filter, obtain filter residue and be washed to pH value for 7~
8, it is modified rice hull active carbon head product to dry, and modified rice hull active carbon is made through 600 DEG C of high-temperature activations.
Activated sludge is obtained according to the following steps described in the present embodiment step one：It is derived from sewage plant secondary sedimentation tank
Returned sludge, after domestication maturation, that is, obtains activated sludge.
The action effect of modified rice husk：To membrane bioreactor, the sludge of modified rice husk-membrane bioreactor coupling device
The organic matter relative molecular weight distribution of mixing liquid carries out METHOD FOR CONTINUOUS DETERMINATION, as a result show modification rice husk add system to 3K~
10KD, 10K~100KD,>The interval organic matters of 100KD tri- (use UV254Value represent) removal effect, more single membrane biological reaction
Device has been respectively increased 3%, 12%, 4%, shows that being modified rice husk has adsorbed partial organic substances and microbial metabolism in mud mixed liquid
Product, mutually assembles, bonds and form biological rice husk in addition, adding the sludge flco after modified rice husk, provided for microorganism
Excellent living environment, enhances sludge activity, makes its degradation capability to organic matter stronger.
Modification rice husk-ultrafiltration membrane bioreactor coupling device described in the present embodiment is that embodiment 1 is provided.
The feature of low-temperature and low turbidity Gao Segao ammonia nitrogen source waters：0~5 DEG C of water temperature, turbidity is 10NTU~15NTU, and colourity is 40
~50 degree, ammonia nitrogen is higher than 1mg/L~1.5mg/L.
Add biological degradable organic carbon source (glucose), make the growth and breeding of microorganism in reactor mixed liquor not by
The limitation of poor nutrient environment, can also promote biological easily biodegradable organicses and the bio-refractory organic matter of accumulation in reactor to produce
Co metabolism effect, excavates the potential of activated sludge, it is ensured that the COD of liquid in membrane bioreactor 10Mn5mg/L~7mg/L, TOC
6mg/L~8mg/L, pH=7.
Operation 3 days, water inlet chroma stability is at 50 degree, and effluent color dilution is at 2 degree~3 degree, and clearance is about 96%；CODMnContent
In 2.5mg/L~2.2mg/L, clearance reaches 70%-80%；NH4- N clearances are of a relatively high when starting, about 95%, water
In total nitrogen content clearance it is relatively low, be 20%~26%.
Effluent color dilution after operation processing in 9 days is at 3 degree~5 degree；Chroma removal rate is 90%~95%；CODMnClearance is
40%~48%, its content is due to change water after the 9th day to cause its clearance rapid drawdown to 40% left side in 2mg/L or so
It is right；NH4- N clearance also decreases, and is 77%~85%, and the clearance of total nitrogen content is 19%~29%, water outlet in water
In total nitrogen content be 3.3mg/L~5.1mg/L.
Operation handles laggard colority of water stabilization for 15 days at 40 degree or so, and effluent color dilution is 0 degree~4 degree；Water outlet CODMnFor
1.62mg/L~1.85mg/L, its clearance is NH in 70%~75%, water4- N is 1mg/L~1.5mg/L, and clearance is
80%~88%, total nitrogen content is 2.2mg/L~2.8mg/L in water, and clearance is 15%~30%.
Operation 30 days, enters colority of water and has been lifted, between 40 degree~45 degree, effluent color dilution is between 1 degree~2 degree；
CODMnClearance is close to 88%, water outlet CODMnValue stabilization is in 1.5mg/L or so；NH in water4Before-N clearance and test run
Total ammon amount in 95% or so, water that remains basically stable for three days is gradually decreased, and clearance is about 25%~40%.
Operation 45 days, effluent color dilution clearance reaches 94%~98%, and effluent color dilution is more stable at 2 degree or so；CODMn
Clearance is 80%-90%；NH in water4- N clearance is stable to be fluctuated, average out to 95% or so, and the clearance of total nitrogen content is
35%~50%.
Operation 90 days, water inlet chroma stability at 37 degree or so, effluent color dilution close to 0, chroma removal rate close to 98%~
100%；CODMnClearance is stable to be fluctuated, average out to 85%；NH in water4- N clearance is stable to be fluctuated, and average out to 96.2%~
98%；Total nitrogen content is stable in 0.7~0.9mg/L in water outlet, and clearance reaches 59%~70%.
Claims (10)
1. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device, it is characterised in that a kind of modified rice husk-milipore filter is biological
Reactor coupling device is by water inlet system, coagulation system, membrane bio-reaction system, outlet system, backwashing system, spoil disposal system
System, sludge recirculation system and robot control system(RCS) composition；
Described water inlet system includes intake pool (1), intake pump (2), feed water flow gauge (3) and water inlet control valve door (4)；
Described coagulation system includes coagulating basin (5), agitator (6), enters medicine-chest (7), coagulant dosage pump (8) and coagulant flow
Gauge (31)；Agitator (6) is set in coagulating basin (5)；
Described membrane bio-reaction system including filler add case (9), membrane bioreactor (10), ultrafiltration UF membrane modules (11),
Aeration tube (12), aeration pump (13), overflow pipe (14), fluid level controller (26) and filler (30)；The ultrafiltration UF membrane modules
(11) vacantly it is arranged in membrane bioreactor (10)；The aeration tube (12) is arranged on below ultrafiltration UF membrane modules (11), is exposed
One end connection aeration pump (13) of tracheae (12)；
Described outlet system is common including the shared pressure gauge (15) of water outlet-backwash, water solenoid valve I (16), water outlet-backwash
With water pump (17), water solenoid valve II (18), water flow meter (19) and discharge bay (20)；
Described backwashing system includes backwash magnetic valve I (21), water outlet-backwash and shares water pump (17), backwash electromagnetism
Valve II (22), water outlet-backwash share pressure gauge (15) and backwash flowmeter (23)；
Described sludge drainage system includes sludge pump (25), spoil disposal valve (29) and sludge-tank (27)；
Described sludge recirculation system includes sludge pump (25) and sludge reflux valve (28)；
Described robot control system(RCS) includes programmable logic controller (PLC) (24), fluid level controller (26), coagulant flow gauge (31), gone out
Water-backwash shares pressure gauge (15), water solenoid valve I (16), water outlet-backwash shared water pump (17), water solenoid valve II
(18), water flow meter (19), backwash magnetic valve I (21), backwash magnetic valve II (22), backwash flowmeter and enter (23)
Water ga(u)ge (3)；
The coagulating basin (5) is separated with membrane bioreactor (10) by overflow wall, and overflow wall highly less than coagulating basin (5) and
Other side walls of membrane bioreactor (10)；
The fluid level controller (26) is vacantly arranged on above ultrafiltration UF membrane modules (11), and the pointer end of fluid level controller (26)
End height is higher than ultrafiltration UF membrane modules (11) water outlet height, less than overflow wall height；
Overfall is set on the side wall of membrane bioreactor (10) non-overflow wall, and the height of overfall is high less than overflow wall
Degree, higher than the pointer end height of fluid level controller (26), overfall is connected with the one end of overflow pipe (14), overflow pipe (14)
The other end is connected with sludge-tank (27)；
The sludge produced by sludge drainage system to membrane bio-reaction system is discharged；
The sludge reflux that membrane bio-reaction system is produced is entered by coagulation system by sludge recirculation system；
Outlet system and backwashing system is controlled to switch by robot control system(RCS)；
The normal process stage：Backwash magnetic valve I (21) and backwash magnetic valve II (22) closing, water solenoid valve I (16) and
Water solenoid valve II (18) is opened, and treatment sewage enters coagulation system by water inlet system, then enters film biology by overflow
Reaction system, the sewage after processing enters outlet system by membrane bio-reaction system；
The backwash stage：Water solenoid valve I (16) and water solenoid valve II (18) are closed, backwash magnetic valve I (21) and recoil
Wash magnetic valve II (22) unlatching, discharge bay (20) storage processing after sewage sequentially pass through backwash magnetic valve I (21), water outlet-
Backwash shares water pump (17), backwash magnetic valve II (22) and backwash flowmeter (23), passes through ultrafiltration UF membrane modules (11)
Delivery port ultrafiltration UF membrane modules (11) are backwashed.
2. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, it is characterised in that wait to locate
Reason sewage is stored in intake pool (1), using intake pump (2) by treatment sewage is by feed water flow gauge (3) and enters water management
In valve (4) feeding coagulating basin (5).
3. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, it is characterised in that coagulation
Agent is stored in into medicine-chest (7), and coagulant is sent into coagulating basin by coagulant flow gauge (31) using coagulant dosage pump (8)
(5) in.
4. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, it is characterised in that filler
(30) it is stored in filler to add in case (9), adding case (9) by filler (30) by filler is added to membrane bioreactor (10)
In.
5. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, it is characterised in that in film
Bioreactor (10) bottom mud mouth is connected by sludge pump (25) and spoil disposal valve (29) with sludge-tank (27), biological in film
Reactor (10) bottom mud mouth is connected by sludge pump (25) and sludge reflux valve (28) with coagulating basin (5).
6. a kind of modified rice husk-ultrafiltration membrane bioreactor coupling device according to claim 1, it is characterised in that described
Ultrafiltration UF membrane modules (11) in Kynoar hollow fiber curtain type film assembly, pH scopes be 2~10；Allow operating pressure be
0.01MPa~0.05MPa；0.02 μm~0.2 μm of membrane aperture；400 μm~450 μm of external diameter, 320 μm~350 μm of internal diameter；Film size
80cm × 1000 piece；Its molecular cut off is 60000~100000；Porosity is 40%~50%.
7. a kind of handle low-temperature and low turbidity Gao Segao ammonia nitrogen source waters using modified rice husk-ultrafiltration membrane bioreactor coupling device
Method, it is characterised in that it is completed according to the following steps：
First, startup stage：Using low-temperature and low turbidity Gao Segao ammonia nitrogens source water as treatment sewage, treatment sewage is added into film life
In thing reactor (10), it is ensured that the liquid level for the treatment of sewage is less than the pointer end of liquid level sensor (26), and floods completely super
UF membrane modules (11) are filtered, are then 15000mg/L~20000mg/L inoculation of activated-sludge by activated sludge concentration, and by filling out
Material adds case (9) and filler (30) is added in membrane bioreactor (10), it is ensured that suspended solid in membrane bioreactor (10)
Concentration is 20000mg/L~25000mg/L, starts aeration pump (13), is aerated using continuous aeration mode, and control film is biological
Liquid dissolved oxygen concentration is 6mg/L~7mg/L in reactor (10)；Intake pump (2), coagulant dosage pump (8) are opened simultaneously, stirred
Mix device (6) and programmable logic controller (PLC) (24), using intake pump (2) by treatment sewage from intake pool (1), using addition as
28L/h is sequentially passed through in feed water flow gauge (3) and water inlet control valve door (4) feeding coagulating basin (5), utilizes coagulant dosage pump
(8) by coagulant from medicine-chest (7) is entered, coagulating basin is sent into by coagulant flow gauge (31) by 20mg/L~25mg/L of dosage
(5) in, mixed using agitator (6) under rotating speed 800r/min, sewage after coagulation in coagulating basin (5) reaches overflow
During wall height, the sewage after coagulation is entered in membrane bioreactor (10) by overflow wall from coagulating basin (5) overflow；Work as membrane bioreaction
When answering the pointer of liquid contact liquid level sensor (26) in device (10), this signal inputs FPGA by liquid level sensor (26)
Controller (24), now programmable logic controller (PLC) (24) control water solenoid valve I (16), water outlet-backwash shares water pump
(17) opened with water solenoid valve II (18), using programmable logic controller (PLC) (24) according to feed water flow gauge (3) and coagulant
Flowmeter (31) records treatment sewage addition and coagulant addition respectively, and sharing water pump (17) in water outlet-backwash opens
Sludge reflux valve (28) is opened while dynamic, and starts sludge pump (25), sludge reflux is carried out, by sludge in coagulating basin (5)
Concentration value control is 500mg/L~900mg/L, and startup stage terminates；
2nd, normal water outlet stage：Continued using intake pump (2) by treatment sewage from intake pool (1), using addition as 28L/h
Sequentially pass through in feed water flow gauge (3) and water inlet control valve door (4) feeding coagulating basin (5), continued using coagulant dosage pump (8)
Coagulant is from medicine-chest (7) is entered, by 10mg/L~15mg/L of dosage by coagulant flow gauge (31) feeding coagulating basin (5)
In, the rotating speed 800r/min of control agitator (6) is 2min in coagulating basin (5) interior hydraulic detention time；And patrolled using programmable
Collect controller (24) and treatment sewage addition and coagulation are recorded according to feed water flow gauge (3) and coagulant flow gauge (31) respectively
Agent addition, aeration pump (13) is persistently aerated using continuous aeration mode, liquid dissolved oxygen in control membrane bioreactor (10)
Concentration is 6mg/L~7mg/L；In order to ensure in membrane bioreactor (10) suspended sediment concentration be 20000mg/L~
25000mg/L, timely additional fillers (30), sewage is sequentially passed through out by the delivery port of ultrafiltration UF membrane modules (11) after processing
Water solenoid valve I (16), water outlet-backwash share water pump (17), water solenoid valve II (18) and water flow meter (19) and enter
In pond (20)；Numeric feedback is constantly given programmable logic controller (PLC) (24) by water flow meter (19), passes through FPGA
Controller (24) adjusting water outlet-backwash shares water pump (17) frequency, it is ensured that using water yield as 130L/m2H~160L/m2·h
Water outlet；Hydraulic detention time is 2h in membrane bioreactor (10)；
3rd, the stage is backwashed：According to water flow meter (19) feedback information, 25min~30min is reached when the continuous effluent time
When, programmable logic controller (PLC) (24) control water solenoid valve I (16) and water solenoid valve II (18) are closed, while controlling recoil
Wash magnetic valve I (21) and backwash magnetic valve II (22) is opened, sewage sequentially passes through recoil after the processing of discharge bay (20) storage
Wash magnetic valve I (21), water outlet-backwash and share water pump (17), backwash magnetic valve II (22) and backwash flowmeter (23), lead to
The delivery port for crossing ultrafiltration UF membrane modules (11) is backwashed to ultrafiltration UF membrane modules (11)；Programmable logic controller (PLC) (24) root
It is 0.4m according to program setting backwash water flow3/m2H~0.5m3/m2H, and it is shared to input a signal into water outlet-backwash
The signal input part of water pump (17), control water outlet-backwash shares water pump (17) frequency converter regulating frequency, it is ensured that with the wash-off that recoils
Water-carrying capacity is 0.4m3/m2H~0.5m3/m2H is backwashed to ultrafiltration UF membrane modules (11), and backwashing water drains into film life
In thing reactor (10), when membrane bioreactor (10) interior liquid level reaches overflow open height, dirt is drained into by overflow pipe (14)
In mud sump (27), backwashing time is controlled in 2min~4min；
4th, the spoil disposal stage：When membrane bioreactor (10) base sludge builds up to aeration tube (12) bottom tube wall, sludge pump is utilized
(25) sludge is drained into sludge-tank (27) through spoil disposal valve (29), is to membrane bioreactor (10) bottom suspended sediment concentration
20000mg/L~25000mg/L；
5th, the Membrane cleaning stage：When water outlet-backwash, which shares pressure gauge (15) numerical value, reaches 0.05MPa, the modified rice husk of closing-super
All systems of membrane filter bioreactor coupling device, take out ultrafiltration UF membrane modules (11), are cleaned.
8. it is according to claim 1 a kind of low using modified rice husk-ultrafiltration membrane bioreactor coupling device processing low temperature
The method of turbid Gao Segao ammonia nitrogens source water, it is characterised in that periodically add organic carbon in step 2 into membrane bioreactor (10)
Source, it is ensured that the COD of liquid in membrane bioreactor (10)Mn5mg/L~7mg/L, TOC 6mg/L~8mg/L, pH=7.
9. it is according to claim 8 a kind of low using modified rice husk-ultrafiltration membrane bioreactor coupling device processing low temperature
The method of turbid Gao Segao ammonia nitrogens source water, it is characterised in that filler described in step one (30) is modified rice hull active carbon, described
Modified rice hull active carbon is obtained according to the following steps：4h is soaked through 1mol/LHCl solution after rice husk removal of impurities, washing, is washed to
PH value is 7~8, is dry, removing K at 100 DEG C in temperature+、Na+、Ca2+、Fe2+、Mg2+, dried rice husk inserts Muffle furnace
Completely cut off 800 DEG C of carbonization 3h of air, 0.2g carbonization rice husks and 20mL 1.5mol/LNaOH solution are heated to reflux 2h, filtered, is obtained
Filter residue is simultaneously washed to pH value for 7~8, and it is modified rice hull active carbon head product to dry, and modified rice is made through 600 DEG C of high-temperature activations
Shell activated carbon.
10. it is according to claim 9 a kind of low using modified rice husk-ultrafiltration membrane bioreactor coupling device processing low temperature
The method of turbid Gao Segao ammonia nitrogens source water, it is characterised in that activated sludge is obtained according to the following steps described in step one：Take
From the returned sludge of sewage plant secondary sedimentation tank, after domestication maturation, that is, activated sludge is obtained.
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