CN102701434B - Combined self-control membrane bioreactor and method for treating low-temperature low-turbidity high-chroma high-ammonia nitrogen source water using same - Google Patents

Combined self-control membrane bioreactor and method for treating low-temperature low-turbidity high-chroma high-ammonia nitrogen source water using same Download PDF

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CN102701434B
CN102701434B CN201210236750XA CN201210236750A CN102701434B CN 102701434 B CN102701434 B CN 102701434B CN 201210236750X A CN201210236750X A CN 201210236750XA CN 201210236750 A CN201210236750 A CN 201210236750A CN 102701434 B CN102701434 B CN 102701434B
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membrane bioreactor
programmable logic
logic controller
pump
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CN102701434A (en
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于水利
孙楠
时文歆
衣雪松
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Harbin Institute of Technology
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Abstract

The invention discloses a combined self-control membrane bioreactor and a method for treating low-temperature low-turbidity high-chroma high-ammonia nitrogen source water using the same, relates to a water treatment reactor and a feed water treatment method, and aims at solving the problem that the existing low-temperature low-turbidity high-chroma high-ammonia nitrogen water treatment methods are high in cost and low in treatment capability. The combined self-control membrane bioreactor consists of a water inlet system, a membrane bioreactor water treatment system, a water outlet system, a backwashing system, a sludge discharge system and a chemical dosing device. The method comprises the steps of: I, firstly starting the combined self-control membrane bioreactor; and II, carrying out full-automatic operation. The combined self-control membrane bioreactor has the following advantages that I, the full-automatic operation is realized, the treatment cost is reduced and the treatment capability is improved; and II, the traditional powdered activated carbon is replaced by modified palygorskite which is low in cost and environment-friendly, so that the soluble organic matters can be effectively removed and the membrane pollution can be effectively slowed down. The combined self-control membrane bioreactor is mainly used for treating low-temperature low-turbidity high-chroma high-ammonia nitrogen source water.

Description

The method of a kind of combined type automatic control membrane bioreactor and the high ammonia nitrogen source water of processing low-temperature and low turbidity high luminance relay thereof
Technical field
The present invention relates to a kind of to water processing reactor and feedwater treatment method.
Background technology
North water system is compared with other water systems of the whole nation, in the geographical position, all there are self characteristics in aspect such as weather, the landform hydrology, soil type (blackland is rich in organic matter), Economic development present situation: 1. northern area reaches 4～6 months winter, nature temperature is lower than zero degree, and water temperature is also below 5 ℃, and turbidity is low in the water; 2. the river often shuttles back and forth in mountain area and knob, and this area forest extensively distributes, and soil is black earth, chernozem and straw mattress soil (being broad sense black earth), and the erosion degree height is one of important source of causing watershed sediment and pollution of area source; 3. pollution of area source is accumulated winter, discharge spring, concentrate on for 6～September summer, ice-bound low water season, river discharge obviously reduced, and the organic pollutant degradation effect is very slow, having prolonged organic pollutant is detained and the time of moving, ice sheet covers and has cut off its volatilization migratory route simultaneously, and the photodissociation ability makes organic pollutant that bigger pollution range and stronger pollution intensity be arranged; To sum up, determined that winter, north water quality presented the obvious characteristic of the high ammonia nitrogen of low-temperature and low turbidity high luminance relay, because natural condition are very unique, be difficult to use for reference the result of study in existing basin; Because northern area Various Seasonal raw water quality changes greatly, caused difficulty for design model and the treatment process of handling structures, so the processing of the high ammonia nitrogen of low-temperature and low turbidity high luminance relay source water is focus and difficult point in the engineering of water treatment always in addition; Meanwhile, the enforcement of new standard has also proposed higher, tighter requirement to safety of drinking water and treatment process; Therefore, it is very necessary to carry out systematic study at the high ammonia nitrogen of low-temperature and low turbidity high chroma source water.
In recent years, membrane technique has been widely used in water treatment field, and wherein, it is rapid especially that micro-filtration and ultra-filtration membrane are used for the tap water production development.Along with the decline of film price, it is expected to replace the conventional tap water production technique of coagulation, precipitation sand filtration and sterilization, becomes one of most important technical renovation in the water treatment field.Membrane bioreactor receives much attention because its processing effluent quality is good.Therefore lot of documents is taked ultra-filtration membrane and coagulation, Powdered Activated Carbon coupling, or takes ultra-filtration membrane and high density powder gac combination technique, and with the treatment effect of decelerating membrane pollution with the raising pollutent, but expense is higher, and processing power is low.
There is the cost height in the high ammonia nitrogen water treatment method of existing low-temperature and low turbidity high luminance relay in sum, and the low problem of processing power.
Summary of the invention
The objective of the invention is to solve the high ammonia nitrogen water treatment method of existing low-temperature and low turbidity high luminance relay and have the cost height, and the low problem of processing power, and a kind of combined type automatic control membrane bioreactor is provided and handles the method for the high ammonia nitrogen source water of low-temperature and low turbidity high luminance relay.
A kind of combined type automatic control membrane bioreactor is by distribution reservoir, intake pump, inlet gage, the flooding velocity meter, the water inlet liquid level sensor, administration device, membrane module, membrane bioreactor, guide shell, aeration tube, gas meter, pneumatic pump, first frequency transformer, water outlet-back flushing three-way solenoid valve, water outlet constant current suction pump, second frequency transformer, the discharge pressure table, the water flow meter, filtered water tank, backwashing pump, the 3rd frequency transformer, the backwashing pressure table, the back flushing under meter, the spoil disposal three-way solenoid valve, sludge pump, mud storage pool, the spoil disposal liquid level sensor, mud valve, programmable logic controller and upper computer are formed, wherein by distribution reservoir, intake pump, inlet gage, flooding velocity meter and water inlet liquid level sensor are formed water inlet system, distribution reservoir is communicated with membrane bioreactor top water-in by intake pump, and the pipeline between intake pump and membrane bioreactor is installed inlet gage and flooding velocity meter, adopt the switch of water inlet liquid level sensor control intake pump, the water inlet liquid level sensor has three probes, is respectively upper limit water-level probe, lower limit water-level probe and lowest water level probe; Wherein by membrane module, membrane bioreactor, guide shell, aeration tube, gas meter and pneumatic pump component film bio-reactor water treatment system, the membrane module top is lower than lowest water level probe sound end, and be suspended from the membrane bioreactor middle part, between membrane module and membrane bioreactor bottom, double aeration tube is set, and aeration tube connects a pneumatic pump, pipeline between pneumatic pump and aeration tube is installed gas meter, between membrane module and membrane bioreactor sidewall guide shell is set; Wherein form outlet system by water outlet-back flushing three-way solenoid valve, water outlet constant current suction pump, discharge pressure table, water flow meter and filtered water tank, the membrane module water outlet links to each other with water outlet-back flushing three-way solenoid valve, water outlet-back flushing three-way solenoid valve links to each other with water-in on the filtered water tank by water outlet constant current suction pump, and the pipeline between water outlet constant current suction pump and filtered water tank is installed discharge pressure table and water flow meter; Wherein form back-purge system by water outlet-back flushing three-way solenoid valve, backwashing pump, backwashing pressure table, back flushing under meter and filtered water tank, water outlet-back flushing three-way solenoid valve links to each other with filtered water tank lower-left water outlet by backwashing pump, and the pipeline between backwashing pump and water outlet-back flushing three-way solenoid valve is installed backwashing pressure table and back flushing under meter; Wherein form sludge drainage system by spoil disposal three-way solenoid valve, sludge pump, mud storage pool, spoil disposal liquid level sensor, mud valve and filtered water tank, mud storage pool links to each other with the spoil disposal three-way solenoid valve by sludge pump, the spoil disposal three-way solenoid valve links to each other with filtered water tank bottom right water outlet with the membrane bioreactor outlet at bottom respectively, a spoil disposal liquid level sensor is installed in mud storage pool, the spoil disposal liquid level sensor has two probes, be respectively that mud stops probe and clear water stops probe, at the pipeline of mud storage pool mud discharging mouth a mud valve be installed; Administration device is installed in the membrane bioreactor top; Utilize the switch situation of programmable logic controller (PLC) controls intake pump and sludge pump, utilize programmable logic controller to pass through first frequency transformer, second frequency transformer and the 3rd frequency transformer are controlled pneumatic pump respectively, the switch situation of water outlet constant current suction pump and backwashing pump, inlet gage, the flooding velocity meter, the water inlet liquid level sensor, gas meter, the discharge pressure table, the water flow meter, the backwashing pressure table, the information that back flushing under meter and spoil disposal liquid level sensor show feeds back to upper computer by programmable logic controller, demonstrates inlet gage at upper computer, the flooding velocity meter, the water inlet liquid level sensor, gas meter, the discharge pressure table, the water flow meter, the backwashing pressure table, the actual information of back flushing under meter and spoil disposal liquid level sensor.
Principle of work: combined type automatic control membrane bioreactor is by upper computer editor water inlet system, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device, then the program that edits is downloaded to programmable logic controller, utilize the switch situation of programmable logic controller (PLC) controls intake pump and sludge pump, utilize programmable logic controller to pass through first frequency transformer, second frequency transformer and the 3rd frequency transformer are controlled pneumatic pump respectively, the switch of water outlet constant current suction pump and backwashing pump and running condition, utilize the concrete situation that is connected of programmable logic controller (PLC) controls water outlet-back flushing three-way solenoid valve and spoil disposal three-way solenoid valve, reach combined type automatic control membrane bioreactor fully automatic operation.
The method of the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay, specifically be to finish according to the following steps: one, start: be under 3 ℃～5 ℃ conditions in temperature, at first the high ammonia nitrogen source water of low-temperature and low turbidity high luminance relay is added in distribution reservoir and the membrane bioreactor, the liquid level of the high ammonia nitrogen source water of pending low-temperature and low turbidity high luminance relay is between upper limit water-level probe sound end and lower limit water-level probe sound end in the membrane bioreactor, the water inlet liquid level sensor is given programmable logic controller with signal feedback, this moment, the programmable logic controller (PLC) controls administration device started, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor, dosage is 30g/L～40g/L, programmable logic controller starts pneumatic pump by control first frequency transformer simultaneously, making aeration tube is that 480L/h～640L/h carries out aeration with the aeration rate, aeration rate shows by gas meter, data feed back to programmable logic controller, and show at upper computer, when if gas meter shows that at upper computer numerical value is lower than 480L/h or is higher than 640L/h, programmable logic controller is regulated to the instruction of first frequency transformer output operating frequency, the rotating speed of control pneumatic pump, till with the aeration rate being 480L/h～640L/h to aeration tube, combined type automatic control this moment membrane bioreactor starts to be finished; Two, fully automatic operation: after the startup of combined type automatic control membrane bioreactor is finished, by upper computer editor water inlet system, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device, then the program that edits is inputed to programmable logic controller, carry out the program that upper computer edits by programmable logic controller, namely utilize the switch situation of programmable logic controller (PLC) controls intake pump and sludge pump, utilize programmable logic controller to pass through first frequency transformer, second frequency transformer and the 3rd frequency transformer are controlled pneumatic pump respectively, the switch situation of water outlet constant current suction pump and backwashing pump, combined type automatic control membrane bioreactor are normally moved the back can collect clear water after obtaining handling at filtered water tank.
Advantage of the present invention: one, combined type automatic control membrane bioreactor of the present invention is controlled by programmable logic controller (PLC), each is controlled function and handles the high ammonia nitrogen source water of low-temperature and low turbidity high luminance relay automatically continuously by the program realization of establishment, reliability is high and simple to operate, reduce processing cost, stronger more in the past than the means of relay controlling suitability that realized by mechanical action, change water treatment process and only need change software parameter, need not to change hardware device, be widely used in medium and small (4t/h is following) Membrane Bioreactor for Wastewater Treatment system; Two, combined type automatic control membrane bioreactor man-machine interface of the present invention is good, debugging, update routine are conveniently, upper computer and programmable logic controller (PLC) but but on-line communication in-service monitoring running status, operating parameter shows the management of covering all at one glance, be convenient to check meter at the upper computer interface, reduce labor intensity of operating staff, save the labor force; Three, combined type automatic control membrane bioreactor of the present invention has self-protective mechanism, when fault occurs, sound and light alarm will occur, and record trouble information, and easy access and information are reviewed; In case gross error appears in system's operation, and is when the situation of superpotential and overcurrent for example occurring, out of service immediately; Four, combined type automatic control membrane bioreactor of the present invention carries out flow and pressure adjusting with frequency transformer, and electric motor starting is steady, reduces the impact to electrical network and equipment, has energy-conservation effect, can also reduce equipment attrition simultaneously, increases the service life; Five, the present invention adopts modified paligorskite to substitute traditional Powdered Activated Carbon, cheap environmental protection, and can effectively remove dissolved organic matter, effective decelerating membrane pollution; Six, the present invention adopts modified paligorskite flocculation sorbent material and membrane bioreactor to unite use, and system is short start time, and is good to index treatment effects such as turbidity, colourity, ammonia nitrogens, reached the purpose of handling the high ammonia nitrogen water of low-temperature and low turbidity high luminance relay; Seven, the present invention moves 15 days clear water turbidity 0.3～0.5NTU after the processing; Chroma removal rate is 91%～95%; UV 254Clearance is 85%～92%; COD MnClearance is 40%～48%; NH 4-N clearance is 39%～46%,
Figure GDA00003202980500041
Average out to 0.042～0.05mg/L; The present invention moves 80 days clear water turbidity＜0.1NTU after the processing; Effluent color dilution is 0～4 degree, and its clearance is 92%～100%; Water outlet UV254 is stabilized in 0.008～0.012cm -1, its average removal rate is 94%～96.43%; Water outlet COD MnBe 2.18～3.02mg/L, its clearance is 50.31%～63.67%; Water outlet NH 4-N is 0.1mg/L～0.15mg/L, and clearance is 96.2%～98%.
Description of drawings
Fig. 1 is the structural representation of embodiment one described combined type automatic control membrane bioreactor; Fig. 2 is that Fig. 1 combined type automatic control membrane bioreactor is that control core concerns synoptic diagram with programmable logic controller (PLC).
Embodiment
Embodiment one: present embodiment is that a kind of combined type automatic control membrane bioreactor is by distribution reservoir 1, intake pump 2, inlet gage 3, flooding velocity meter 4, water inlet liquid level sensor 5, administration device 6, membrane module 7, membrane bioreactor 8, guide shell 9, aeration tube 10, gas meter 11, pneumatic pump 12, first frequency transformer 13, water outlet-back flushing three-way solenoid valve 14, water outlet constant current suction pump 15, second frequency transformer 16, discharge pressure table 17, water flow meter 18, filtered water tank 19, backwashing pump 20, the 3rd frequency transformer 21, backwashing pressure table 22, back flushing under meter 23, spoil disposal three-way solenoid valve 24, sludge pump 25, mud storage pool 26, spoil disposal liquid level sensor 27, mud valve 28, programmable logic controller (PLC) 29 and upper computer (IFIX software) 30 formed, wherein by distribution reservoir 1, intake pump 2, inlet gage 3, flooding velocity meter 4 and water inlet liquid level sensor 5 are formed water inlet system, distribution reservoir 1 is communicated with membrane bioreactor 8 top water-ins by intake pump 2, and the pipeline between intake pump 2 and membrane bioreactor 8 is installed inlet gage 3 and flooding velocity meter 4, adopt the switch of water inlet liquid level sensor 5 control intake pumps 2, water inlet liquid level sensor 5 has three probes, is respectively upper limit water-level probe 5-1, lower limit water-level probe 5-2 and lowest water level probe 5-3; Wherein by membrane module 7, membrane bioreactor 8, guide shell 9, aeration tube 10, gas meter 11 and pneumatic pump 12 component film bio-reactor water treatment systems, membrane module 7 tops are lower than lowest water level probe 5-3 sound end, and be suspended from membrane bioreactor 8 middle parts, between membrane module 7 and membrane bioreactor 8 bottoms, double aeration tube 10 is set, and aeration tube 10 connects a pneumatic pump 12, pipeline between pneumatic pump 12 and aeration tube 10 is installed gas meter 11, between membrane module 7 and membrane bioreactor 8 sidewalls guide shell 9 is set; Wherein form outlet system by water outlet-back flushing three-way solenoid valve 14, water outlet constant current suction pump 15, discharge pressure table 17, water flow meter 18 and filtered water tank 19, membrane module 7 water outlets link to each other with water outlet-back flushing three-way solenoid valve 14, water outlet-back flushing three-way solenoid valve 14 links to each other with water-in on the filtered water tank 19 by water outlet constant current suction pump 15, and the pipeline between water outlet constant current suction pump 15 and filtered water tank 19 is installed discharge pressure table 17 and water flow meter 18; Wherein form back-purge system by water outlet-back flushing three-way solenoid valve 14, backwashing pump 20, backwashing pressure table 22, back flushing under meter 23 and filtered water tank 19, water outlet-back flushing three-way solenoid valve 14 links to each other with filtered water tank 19 lower-left water outlets by backwashing pump 20, and the pipeline between backwashing pump 20 and water outlet-back flushing three-way solenoid valve 14 is installed backwashing pressure table 22 and back flushing under meter 23; Wherein by spoil disposal three-way solenoid valve 24, sludge pump 25, mud storage pool 26, spoil disposal liquid level sensor 27, mud valve 28 and filtered water tank 19 are formed sludge drainage system, mud storage pool 26 links to each other with the spoil disposal three-way solenoid valve by sludge pump 25, spoil disposal three-way solenoid valve 24 links to each other with filtered water tank 19 bottom right water outlets with membrane bioreactor 8 outlet at bottoms respectively, a spoil disposal liquid level sensor 27 is installed in mud storage pool 26, spoil disposal liquid level sensor 27 has two probes, be respectively that mud stops probe 27-1 and clear water stops probe 27-2, at the pipeline of mud storage pool 26 mud discharging mouths a mud valve 28 be installed; Administration device 6 is installed in membrane bioreactor 8 tops; Utilize the switch situation of programmable logic controller (PLC) 29 control intake pumps 2 and sludge pump 25, utilize programmable logic controller (PLC) 29 by first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21 are controlled pneumatic pump 12 respectively, switch and the running condition of water outlet constant current suction pump 15 and backwashing pump 20, inlet gage 3, flooding velocity meter 4, water inlet liquid level sensor 5, gas meter 11, discharge pressure table 17, water flow meter 18, backwashing pressure table 22, the information that back flushing under meter 23 and spoil disposal liquid level sensor 27 show feeds back to upper computer (IFIX software) 30 by programmable logic controller (PLC) 29, demonstrates inlet gage 3 at upper computer (IFIX software) 30, flooding velocity meter 4, water inlet liquid level sensor 5, gas meter 11, discharge pressure table 17, water flow meter 18, backwashing pressure table 22, the actual information of back flushing under meter 23 and spoil disposal liquid level sensor 27.
Principle of work: combined type automatic control membrane bioreactor is by upper computer (IFIX software) 30 editor's water inlet systems, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device 6, then the program that edits is inputed to programmable logic controller (PLC) 29, carry out upper computer (IFIX software) 30 programs that edit by programmable logic controller (PLC) 29, namely utilize the switch situation of programmable logic controller (PLC) 29 control intake pumps 2 and sludge pump 25, utilize programmable logic controller (PLC) 29 by first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21 are controlled pneumatic pump 12 respectively, switch and the running condition of water outlet constant current suction pump 15 and backwashing pump 20, utilize the concrete situation that is connected of programmable logic controller (PLC) 29 control water outlet-back flushing three-way solenoid valves 14 and spoil disposal three-way solenoid valve 24, reach combined type automatic control membrane bioreactor fully automatic operation.
The described combined type automatic control of present embodiment membrane bioreactor is core with programmable logic controller (PLC) 29, by the constant current control of PLC and upper computer 30, first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21 communications realization system, be that control core concerns synoptic diagram such as Fig. 2 with programmable logic controller (PLC) 29.The monitoring software of upper computer 30 adopts the IFIX3.5 integrated software package, mainly finish the demonstration of technical process picture, editor's water inlet system, the Membrane Bioreactor for Wastewater Treatment system, outlet system, back-purge system, the program of sludge drainage system and administration device 6 running conditions, gather the parameter value in each system in real time, and on picture, dynamically show inlet gage 3, flooding velocity meter 4, water inlet liquid level sensor 5, gas meter 11, discharge pressure table 17, water flow meter 18, backwashing pressure table 22, the actual value of back flushing under meter 23 and spoil disposal liquid level sensor 27, automatically preserve each point value, automatically report to the police, statistics is printed, form etc.; Upper computer 30 inputs to programmable logic controller (PLC) 29 with the program that edits, programmable logic controller (PLC) 29 main data gathering, data filtering, the ranges of being responsible for the various device running status transform, handle by realization, the emergency situation of editor steering order that send or lower computer inside for upper computer, thereby the monitoring of real fortune present condition, parameter setting are revised, and finish the automatic control of each system.PLC adopts OMRON company standard product, this PLC is made up of with power panel central processing unit (CPU board), I/O (I/O) part, can select RS232 or RS422/485 standard serial communication port according to actual needs for use, upper computer carries out data interaction by serial ports and PLC; Can select the RS422/485 mode when upper computer and PLC distance is far away, maximum distance can reach 500 meters.Ethernet interface be can also select when needing remote monitoring, intranet or internet inserted.According to this system process requirement, carrying out PLC I/O (I/O) adds up: 1. switching value input (AI): for the operation feedback that receives membrane bioreactor upper limit water-level probe 5-1, lower limit water-level probe 5-2, lowest water level probe 5-, mud termination probe 27-1, clear water termination probe 27-2, intake pump 2, pneumatic pump 12, water outlet constant current suction pump 15, backwashing pump 20 and sludge pump 25, the numerary signal of the fault feedback of intake pump 2, pneumatic pump 12, water outlet constant current suction pump 15, backwashing pump 20 and sludge pump 25 amounts to 15 points.2. switching value output (AO): be used for the numerary signal of the start and stop control of control administration device 6, water outlet-back flushing three-way solenoid valve 14, spoil disposal three-way solenoid valve 24, sound and light alarm, intake pump 2, pneumatic pump 12, water outlet constant current suction pump 15, backwashing pump 20 and sludge pump 25, amount to 9 points.3. analog quantity input (DI): be used for gathering the electric current of intake pressure, flooding velocity, gas flow, discharge pressure, water flow, backwashing pressure, back flushing flow, first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21, the simulating signal of rotary speed parameter feedback, amount to 13 tunnel.4. analog quantity output (DO): be used for given by the frequency conversion of analog quantity control pneumatic pump, go out that pump variable frequency is given, the backwashing pump frequency conversion is given, amount to 3 the tunnel.The main frame of PLC is selected OMRON CP1H-X40DR-A model for use, also needs to join 4 of CP1W-AD041 analog quantity load modules totally 16 tunnel in addition, 1 of CP1W-DA041 analog output module totally 4 tunnel.This configuration has switching value and imports 24 points, and switching value is exported 16 points, and analog quantity imports 16 the tunnel, and analog quantity exports 4 the tunnel, can satisfy the demands fully, also leaves the part surplus, and convenience is safeguarded this system in the future and upgraded.
The described combined type automatic control of present embodiment membrane bioreactor man-machine interface is good, debugging, update routine are conveniently, upper computer and programmable logic controller (PLC) but but on-line communication in-service monitoring running status, operating parameter shows the management of covering all at one glance, be convenient to check meter at the upper computer interface, reduce labor intensity of operating staff, save the labor force.
The described combined type automatic control of present embodiment membrane bioreactor has self-protective mechanism, when fault occurs, sound and light alarm will occur, and record trouble information, and easy access and information are reviewed; In case gross error appears in system's operation, and is when the situation of superpotential and overcurrent for example occurring, out of service immediately.
The described combined type automatic control of present embodiment membrane bioreactor carries out flow with frequency transformer and pressure is regulated, and electric motor starting is steady, reduces the impact to electrical network and equipment, has energy-conservation effect, can also reduce equipment attrition simultaneously, increases the service life.
Embodiment two: present embodiment is the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay, specifically be to finish according to the following steps: one, start: at first high ammonia nitrogen source water adds in distribution reservoir 1 and the membrane bioreactor 8 with the low-temperature and low turbidity high luminance relay to be 3 ℃～5 ℃ in temperature, the liquid level for the treatment of sewage is between upper limit water-level probe 5-1 sound end and lower limit water-level probe 5-2 sound end in the membrane bioreactor 8, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with signal feedback, programmable logic controller this moment (PLC) 29 control administration devices 6 start, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor 8, dosage is 30g/L～40g/L, programmable logic controller (PLC) 29 starts aerator pump 12 by control first frequency transformer 13 simultaneously, making aeration tube 10 is that 480L/h～640L/h carries out aeration with the aeration rate, aeration rate shows by air flowmeter 11, data feed back to programmable logic controller (PLC) 29, and show at upper computer (IFIX software) 30, when if air flowmeter 11 shows that at upper computer (IFIX software) 30 numerical value is lower than 480L/h or is higher than 640L/h, programmable logic controller (PLC) 29 is regulated to frequency transformer 12 output operating frequency instructions, the rotating speed of control aerator pump 12, till with the aeration rate being 480L/h～640L/h to aeration tube 10, combined type automatic control this moment membrane bioreactor starts to be finished; Two, fully automatic operation: after the startup of combined type automatic control membrane bioreactor is finished, by upper computer (IFIX software) 30 editor's water inlet systems, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device 6, then the program that edits is inputed to programmable logic controller (PLC) 29, carry out upper computer (IFIX software) 30 programs that edit by programmable logic controller (PLC) 29, namely utilize the switch situation of programmable logic controller (PLC) 29 control intake pumps 2 and sludge pump 25, utilize programmable logic controller (PLC) 29 by first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21 are controlled pneumatic pump 12 respectively, switch and the running condition of water outlet constant current suction pump 15 and backwashing pump 20, combined type automatic control membrane bioreactor are normally moved the back can collect clear water after obtaining handling at filtered water tank 19.
When the actual difference that shows inlet gages 3 and discharge pressure table 15 at upper computer (IFIX software) 30 during greater than 0.05MPa, upper computer (IFIX software) 30 presents grave warning, programmable logic controller this moment (PLC) 29 all operational systems of control combined type automatic control membrane bioreactor are closed, flushing with clean water once in the taking-up membrane module 7 elder generations employing filtered water tank 19, use 2% soaking with sodium hydroxide 5 hours then, soak with 0.5% clorox again and removed Organic pollutants in 3 hours, take out the back adopt distilled water clean to water outlet pH be till 7 ± 0.1, membrane module 7 after will cleaning is then reinstalled in the membrane bioreactor 8, and restart combined type automatic control membrane bioreactor, carry out work.
Embodiment three: the difference of present embodiment and embodiment two is: the flocculation of modified paligorskite described in step 1 sorbent material specifically is to prepare according to the following steps: one, purify: at first natural polygorskite and deionized water are by mass ratio 1: (18～99) are added to natural polygorskite in the deionized water, low whipping speed is dispersed with stirring 10min～30min under 1000r/min～10000r/min then, obtain clay slip, again clay slip is placed whizzer, and be centrifugation 10min～20min under 4000r/min～12000r/min at centrifugal rotational speed, obtain the canescence clay puddle through separation, and be to dry to constant weight under 80 ℃～120 ℃ in temperature, after pulverizing 200 mesh sieves again, namely obtaining particle diameter is polygorskite behind the following purifying of 200 orders; Two, load: at first be that to be dissolved in volume fraction be in 2% the glacial acetic acid for 85%～95% chitosan with deacetylation, and it is 20 ℃～100 ℃ in temperature, mixing speed is to be stirred to dissolving fully under 200r/min～400r/min, be that to add particle diameter be polygorskite behind the purifying below 200 orders for 10g/min～50g/min with the speed of adding then, and it is 20 ℃～100 ℃ in temperature, mixing speed is to continue to stir 2h～4h under 200r/min～400r/min, obtain suspension, employing concentration is that the NaOH of 0.5mol/L～1.5mol/L transfers to neutrality with suspension, be centrifugation 10min～20min under 4000r/min～12000r/min at centrifugal rotational speed then, and the solid that centrifugation is obtained adopts deionized water wash 4～6 times, solid after will washing then is 60 ℃～110 ℃ oven dry 12h～24h in temperature, after pulverizing 200 mesh sieves again, namely obtain modified paligorskite flocculation sorbent material; Deacetylation described in the step 2 is that 85%～95% chitosan mass and volume fraction are that the ratio of 2% glacial acetic acid volume is 1g: (30mL～120mL); The mass ratio that adds particle diameter described in the step 2 and be polygorskite and deacetylation behind the following purifying of 200 orders and be 85%～95% chitosan is (5～20): 1.Other are identical with embodiment two.
Embodiment four: present embodiment and one of embodiment two or three difference are: upper computer described in the step 2 (IFIX software) 30 editor's water inlet system running conditions, specifying information is as follows: liquid level is lower than the into lower limit water-level probe 5-2 sound end of water liquid level sensor 5 in membrane bioreactor 8, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, programmable logic controller (PLC) 29 control intake pumps 2 are opened, intake pump 2 is with in the high ammonia nitrogen source water of the low-temperature and low turbidity high luminance relay suction membrane bioreactor 8 in the distribution reservoir 1, when liquid level in the membrane bioreactor 8 touches the upper limit water-level probe 5-1 sound end of water liquid level sensor 5 into, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, programmable logic controller (PLC) 29 control intake pumps 2 are closed, when if distribution reservoir 1 amount of the reserve water is not enough, when being tensimeter 3 with the numerical value of under meter 4 indications much smaller than regime values, this message feedback is given programmed logic controller (PLC), and present at upper computer (IFIX software) 30, the tensimeter 3 that presents when upper computer 30 and under meter 4 indication numerical value are during much smaller than regime values, upper computer (IFIX software) 30 shows alarm, if in time handle, membrane bioreactor 8 interior liquid levels are lower than when into the lowest water level of water liquid level sensor 5 is popped one's head in the 5-3 sound end, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, present grave warning at upper computer (IFIX software) 30, programmable logic controller this moment (PLC) 29 all operational systems of control combined type automatic control membrane bioreactor are closed.Other are identical with embodiment two or three.
Embodiment five: one of present embodiment and embodiment two to four difference is: upper computer described in the step 2 (IFIX software) 30 editor's membrane bioreactor water treatment system running conditions, specifying information is as follows: when grave warning occurring except upper computer (IFIX software) 30, need close sewage disposal system, otherwise membrane bioreactor water treatment system continuous service in combined type automatic control membrane bioreactor operational process, namely wherein by membrane module 7, membrane bioreactor 8, guide shell 9, aeration tube 10, gas meter 11 and pneumatic pump 12 component film bio-reactor water treatment systems, be that aerator pump 12 remains opened condition, it is that 480L/h～640L/h carries out aeration that aeration tube 10 is continued with the aeration rate.Other are identical with embodiment two to four.
Embodiment six: one of present embodiment and embodiment two to five difference is: upper computer described in the step 2 (IFIX software) 30 edits out water system running condition, specifying information is as follows: when the time is set to time of pumping, programmable logic controller (PLC) 29 control water outlet-back flushing three-way solenoid valves 14 are communicated with water outlet constant current suction pump 15, and control water outlet-back flushing three-way solenoid valve 14 disconnects with backwashing pump 20, programmable logic controller (PLC) 29 is opened by the 16 control water outlet constant current suction pumps 15 of second frequency transformer simultaneously, and programmable logic controller (PLC) 29 cuts out by the 3rd frequency transformer 21 control backwashing pumps 20, the clear water that filtration obtains from membrane module 7 water outlets through water outlet-back flushing three-way solenoid valve 14, water outlet constant current suction pump 15 enters in the filtered water tank 19 with filtered water tank 19 water-ins, the single time of pumping is 40min～60min, and membrane flux is 150L/m 2H～250L/m 2H is if water flow meter 18 shows that at upper computer (IFIX software) 30 numerical value is lower than 150L/m 2H or be higher than 250L/m 2During h, programmable logic controller (PLC) 29 is regulated to the 16 output operating frequencys instructions of second frequency transformer, the rotating speed of control water outlet constant current suction pump 15, to membrane flux be 150L/m 2H～250L/m 2Till the h.Other are identical with embodiment two to five.
Embodiment seven: one of present embodiment and embodiment two to six difference is: upper computer described in the step 2 (IFIX software) 30 editor's back-purge system running conditions, specifying information is as follows: when the time is set to backwashing time, programmable logic controller (PLC) 29 control water outlet-back flushing three-way solenoid valves 14 are communicated with backwashing pump 20, and control water outlet-back flushing three-way solenoid valve 14 disconnects with water outlet constant current suction pump 15, programmable logic controller (PLC) 29 is opened by the 3rd frequency transformer 21 control backwashing pumps 20 simultaneously, and programmable logic controller (PLC) 29 cuts out by the 16 control water outlet constant current suction pumps 15 of the 3rd frequency transformer, with back flushing water yield 1.05m 3/ m 2H～1.4m 3/ m 2H extracts the clear water in the filtered water tank 19 out from filtered water tank 19 lower-left water outlets, membrane module 7 is carried out back flushing, and the single backwashing time is 60s～120s, if back flushing under meter 23 shows that at upper computer (IFIX software) 30 numerical value is lower than 1.05m 3/ m 2H or be higher than 1.4m 3/ m 2During h, programmable logic controller (PLC) 29 is regulated to the 21 output operating frequency instructions of second frequency transformer, and the rotating speed of control backwashing pump 20 is to back flushing water yield 1.05m 3/ m 2H～1.4m 3/ m 2Till the h; Programmable logic controller (PLC) 29 settings are water outlet-backwashing period with a water outlet time and a backwashing time sum, back and forth start outlet system and back-purge system in the operational process, back flushing next time began when namely a time of pumping finished, and one time backwashing time finishes the while beginning of drawing water next time.Other are identical with embodiment two to six.
Embodiment eight: one of present embodiment and embodiment two to seven difference is: upper computer described in the step 2 (IFIX software) 30 editor's sludge drainage system running conditions, specifying information is as follows: combined type automatic control membrane bioreactor will regularly carry out spoil disposal in operational process, combined type automatic control membrane bioreactor is set, and spoil disposal is once when operation 2000～3000 water outlets-backwashing period, namely after finishing, the backwashing time of operation 2000～3000 water outlets-backwashing period enters the spoil disposal time, and this moment, outlet system was out of service, and outlet system continues operation again after the spoil disposal time finishes; Be set to spoil disposal during the time when the time, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 are communicated with membrane bioreactor 8 bottom mud discharging mouths, and spoil disposal three-way solenoid valve 24 disconnects with clean water basin 19 bottom right water outlets, mud drains in the mud storage pool 26 through spoil disposal three-way solenoid valve 24 and sludge pump 25, when the mud face touches the mud termination probe 27-1 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 disconnect with membrane bioreactor 8 bottom mud discharging mouths, and be connected with filtered water tank 19 bottom right water outlets, the clear water of filtered water tank 19 is through spoil disposal three-way solenoid valve 24, sludge pump 25 drains in the mud storage pool 26, when the mud face touches the clear water termination probe 27-2 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 are all closed with sludge pump 25, and the sludge drainage system operation is once finished.Other are identical with embodiment two to seven.
Embodiment nine: one of present embodiment and embodiment two to eight difference is: described upper computer described in the step 2 (IFIX software) 30 editor's administration devices 6 running conditions, specifying information is as follows: when the mud face touches the clear water termination probe 27-2 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control (6) control administration devices 6, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor 8, when dosage when being 6g/L～10g/L programmable logic controller (PLC) 29 control administration devices 6 close.Other are identical with embodiment two to eight.
Adopt following verification experimental verification effect of the present invention:
Test one: the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay, specifically be to finish according to the following steps: one, start: be under 4 ℃ in temperature, at first the high ammonia nitrogen source water of low-temperature and low turbidity high luminance relay is added in distribution reservoir 1 and the membrane bioreactor 8, the liquid level of the high ammonia nitrogen source water of pending low-temperature and low turbidity high luminance relay is between upper limit water-level probe 5-1 sound end and lower limit water-level probe 5-2 sound end in the membrane bioreactor 8, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with signal feedback, programmable logic controller this moment (PLC) 29 control administration devices 6 start, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor 8, dosage is 35g/L, programmable logic controller (PLC) 29 starts aerator pump 12 by control first frequency transformer 13 simultaneously, making aeration tube 10 is that 560L/h carries out aeration with the aeration rate, aeration rate shows by air flowmeter 11, data feed back to programmable logic controller (PLC) 29, and show at upper computer (IFIX software) 30, when if air flowmeter 11 is lower than or is higher than 560L/h at upper computer (IFIX software) 30 demonstration numerical value, programmable logic controller (PLC) 29 is regulated to frequency transformer 12 output operating frequency instructions, the rotating speed of control aerator pump 12, till with the aeration rate being 560L/h to aeration tube 10, combined type automatic control this moment membrane bioreactor starts to be finished; Two, fully automatic operation: after the startup of combined type automatic control membrane bioreactor is finished, by upper computer (IFIX software) 30 editor's water inlet systems, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device 6, then the program that edits is inputed to programmable logic controller (PLC) 29, carry out upper computer (IFIX software) 30 programs that edit by programmable logic controller (PLC) 29, namely utilize the switch situation of programmable logic controller (PLC) 29 control intake pumps 2 and sludge pump 25, utilize programmable logic controller (PLC) 29 by first frequency transformer 13, second frequency transformer 16 and the 3rd frequency transformer 21 are controlled pneumatic pump 12 respectively, switch and the running condition of water outlet constant current suction pump 15 and backwashing pump 20, combined type automatic control membrane bioreactor are normally moved the back can collect clear water after obtaining handling at filtered water tank 19.
The flocculation of modified paligorskite described in this testing sequence one sorbent material specifically prepares according to the following steps: one, purify: at first natural polygorskite and deionized water are added to natural polygorskite in the deionized water by mass ratio 5: 95, low whipping speed is dispersed with stirring 15min under the 10000r/min then, obtain clay slip, again clay slip is placed whizzer, and be centrifugation 10min under the 12000r/min at centrifugal rotational speed, obtain the canescence clay puddle through separation, and be to dry to constant weight under 100 ℃ in temperature, after pulverizing 200 mesh sieves again, namely obtaining particle diameter is polygorskite behind the following purifying of 200 orders; Two, load: at first be that to be dissolved in the 150mL volume fraction be in 2% the glacial acetic acid for 95% chitosan with the 2.5g deacetylation, and it is 60 ℃ in temperature, mixing speed is to stir 4h under the 400r/min, be that to add the 25g particle diameter be polygorskite behind the purifying below 200 orders to 10g/min with the speed of adding then, and it is 60 ℃ in temperature, mixing speed is to continue to stir 4h under the 400r/min, obtain suspension, employing concentration is that the NaOH of 1.0mol/L transfers to neutrality with suspension, be centrifugation 10minmin under the 12000r/min at centrifugal rotational speed then, and the solid that centrifugation is obtained adopts deionized water wash 6 times, solid after will washing then is 80 ℃ of oven dry 18h in temperature, after pulverizing 200 mesh sieves again, namely obtain modified paligorskite flocculation sorbent material.
Upper computer described in this testing sequence two (IFIX software) 30 editor's water inlet system running conditions, specifying information is as follows: when liquid level in the membrane bioreactor 8 is lower than the lower limit water-level probe 5-2 sound end of water liquid level sensor 5 into, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, programmable logic controller (PLC) 29 control intake pumps 2 are opened, intake pump 2 is with in the high ammonia nitrogen source water of the low-temperature and low turbidity high luminance relay suction membrane bioreactor 8 in the distribution reservoir 1, when liquid level in the membrane bioreactor 8 touches the upper limit water-level probe 5-1 sound end of water liquid level sensor 5 into, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, programmable logic controller (PLC) 29 control intake pumps 2 are closed, when if distribution reservoir 1 amount of the reserve water is not enough, when being tensimeter 3 with the numerical value of under meter 4 indications much smaller than regime values, this message feedback is given programmed logic controller (PLC), and present at upper computer (IFIX software) 30, the tensimeter 3 that presents when upper computer 30 and under meter 4 indication numerical value are during much smaller than regime values, upper computer (IFIX software) 30 shows alarm, if in time handle, membrane bioreactor 8 interior liquid levels are lower than when into the lowest water level of water liquid level sensor 5 is popped one's head in the 5-3 sound end, water inlet liquid level sensor 5 is given programmable logic controller (PLC) 29 with message feedback, present grave warning at upper computer (IFIX software) 30, programmable logic controller this moment (PLC) 29 control total systems are closed.
Upper computer described in this testing sequence two (IFIX software) 30 editor's membrane bioreactor water treatment system running conditions, specifying information is as follows: when grave warning occurring except upper computer (IFIX software) 30, need close sewage disposal system, otherwise membrane bioreactor water treatment system continuous service in combined type automatic control membrane bioreactor operational process, namely wherein by membrane module 7, membrane bioreactor 8, guide shell 9, aeration tube 10, gas meter 11 and pneumatic pump 12 component film bio-reactor water treatment systems, be that aerator pump 12 remains opened condition, it is that 560L/h carries out aeration that aeration tube 10 is continued with the aeration rate.
Upper computer described in this testing sequence two (IFIX software) 30 edits out water system running condition, specifying information is as follows: when the time is set to time of pumping, programmable logic controller (PLC) 29 control water outlet-back flushing three-way solenoid valves 14 are communicated with water outlet constant current suction pump 15, and control water outlet-back flushing three-way solenoid valve 14 disconnects with backwashing pump 20, programmable logic controller (PLC) 29 is opened by the 16 control water outlet constant current suction pumps 15 of second frequency transformer simultaneously, and programmable logic controller (PLC) 29 cuts out by the 3rd frequency transformer 21 control backwashing pumps 20, the clear water that filtration obtains from membrane module 7 water outlets through water outlet-back flushing three-way solenoid valve 14, water outlet constant current suction pump 15 enters in the filtered water tank 19 with filtered water tank 19 water-ins, the single time of pumping is 50min, and membrane flux is 200L/m 2H is if water flow meter 18 shows that at upper computer (IFIX software) 30 numerical value is below or above 200L/m 2During h, programmable logic controller (PLC) 29 is regulated to the 16 output operating frequencys instructions of second frequency transformer, the rotating speed of control water outlet constant current suction pump 15, to membrane flux be 200L/m 2Till the h.
Upper computer described in this testing sequence two (IFIX software) 30 editor's back-purge system running conditions, specifying information is as follows: when the time is set to backwashing time, programmable logic controller (PLC) 29 control water outlet-back flushing three-way solenoid valves 14 are communicated with backwashing pump 20, and control water outlet-back flushing three-way solenoid valve 14 disconnects with water outlet constant current suction pump 15, programmable logic controller (PLC) 29 is opened by the 3rd frequency transformer 21 control backwashing pumps 20 simultaneously, and programmable logic controller (PLC) 29 cuts out by the 16 control water outlet constant current suction pumps 15 of the 3rd frequency transformer, with back flushing water yield 1.25m 3/ m 2H extracts the clear water in the filtered water tank 19 out from filtered water tank 19 lower-left water outlets, membrane module 7 is carried out back flushing, and the single backwashing time is 90s, if back flushing under meter 23 shows that at upper computer (IFIX software) 30 numerical value is below or above 1.25m 3/ m 2During h, programmable logic controller (PLC) 29 is regulated to the 21 output operating frequency instructions of second frequency transformer, and the rotating speed of control backwashing pump 20 is to back flushing water yield 1.25m 3/ m 2H ends; The temporal summation that programmable logic controller (PLC) 29 arranges with a water outlet time and a backwashing time is water outlet-backwashing period, back and forth start outlet system and back-purge system in the operational process, back flushing next time began when namely a time of pumping finished, and one time backwashing time finishes the while beginning of drawing water next time.
Upper computer described in this testing sequence two (IFIX software) 30 editor's sludge drainage system running conditions, specifying information is as follows: combined type automatic control membrane bioreactor will regularly carry out spoil disposal in operational process, combined type automatic control membrane bioreactor is set, and spoil disposal is once when operation 2500 water outlets-backwashing period, namely after finishing, the backwashing time of operation 2500 water outlets-backwashing period enters the spoil disposal time, and outlet system is out of service, and outlet system continues operation again after the spoil disposal time finishes; Be set to spoil disposal during the time when the time, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 are communicated with membrane bioreactor 8 bottom mud discharging mouths, and spoil disposal three-way solenoid valve 24 disconnects with clean water basin 19 bottom right water outlets, mud drains in the mud storage pool 26 through spoil disposal three-way solenoid valve 24 and sludge pump 25, when the mud face touches the mud termination probe 27-1 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 disconnect with membrane bioreactor 8 bottom mud discharging mouths, and be connected with filtered water tank 19 bottom right water outlets, the clear water of filtered water tank 19 is through spoil disposal three-way solenoid valve 24, sludge pump 25 drains in the mud storage pool 26, when the mud face touches the clear water termination probe 27-2 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control spoil disposal three-way solenoid valves 24 are all closed with sludge pump 25, and the sludge drainage system operation is once finished.
Described upper computer described in this testing sequence two (IFIX software) 30 editor's administration devices 6 running conditions, specifying information is as follows: when the mud face touches the clear water termination probe 27-2 sound end of spoil disposal liquid level sensor 27, spoil disposal liquid level sensor 27 with signal feedback to programmable logic controller (PLC) 29, programmable logic controller (PLC) 29 control (6) control administration devices 6, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor 8, and programmable logic controller when dosage is 8g/L (PLC) 29 control administration devices 6 are closed.
This tests the high ammonia nitrogen source water of described low-temperature and low turbidity high luminance relay turbidity 5～10NTU, UV 2540.205～0.222, colourity 50～70 degree, COD Mn5～6mg/L, NH 4-N4～5mg/L,
Figure GDA00003202980500121
Average 0.010～0.014mg/L, PH are 8～9; Clear water turbidity 0.3～0.5NTU after this test run was handled in 15 days; Chroma removal rate is 91%～95%; UV 254Clearance is 85%～92%; COD MnClearance is 40%～48%; NH 4-N clearance is 39%～46%,
Figure GDA00003202980500131
Average out to 0.042～0.05mg/L; Clear water turbidity＜0.1NTU after this test run was handled in 80 days; Effluent color dilution is 0～4 degree, and its clearance is 92%～100%; Water outlet UV254 is stabilized in 0.008～0.012cm -1, its average removal rate is 94%～96.43%; Water outlet COD MnBe 2.18～3.02mg/L, its clearance is 50.31%～63.67%; Water outlet NH 4-N is 0.1mg/L～0.15mg/L, and clearance is 96.2%～98%.

Claims (9)

1. combined type automatic control membrane bioreactor, it is characterized in that combined type automatic control membrane bioreactor is by distribution reservoir (1), intake pump (2), inlet gage (3), flooding velocity meter (4), water inlet liquid level sensor (5), administration device (6), membrane module (7), membrane bioreactor (8), guide shell (9), aeration tube (10), gas meter (11), pneumatic pump (12), first frequency transformer (13), water outlet-back flushing three-way solenoid valve (14), water outlet constant current suction pump (15), second frequency transformer (16), discharge pressure table (17), water flow meter (18), filtered water tank (19), backwashing pump (20), the 3rd frequency transformer (21), backwashing pressure table (22), back flushing under meter (23), spoil disposal three-way solenoid valve (24), sludge pump (25), mud storage pool (26), spoil disposal liquid level sensor (27), mud valve (28), programmable logic controller (29) and upper computer (30) are formed, wherein by distribution reservoir (1), intake pump (2), inlet gage (3), flooding velocity meter (4) and water inlet liquid level sensor (5) are formed water inlet system, distribution reservoir (1) is communicated with membrane bioreactor (8) top water-in by intake pump (2), and the pipeline between intake pump (2) and membrane bioreactor (8) is installed inlet gage (3) and flooding velocity meter (4), adopt the switch of water inlet liquid level sensor (5) control intake pump (2), water inlet liquid level sensor (5) has three probes, is respectively upper limit water-level probe (5-1), lower limit water-level probe (5-2) and lowest water level probe (5-3); Wherein by membrane module (7), membrane bioreactor (8), guide shell (9), aeration tube (10), gas meter (11) and pneumatic pump (12) component film bio-reactor water treatment system, membrane module (7) top is lower than lowest water level probe (5-3) sound end, and be suspended from membrane bioreactor (8) middle part, between membrane module (7) and membrane bioreactor (8) bottom, double aeration tube (10) is set, and aeration tube (10) connects a pneumatic pump (12), pipeline between pneumatic pump (12) and aeration tube (10) is installed gas meter (11), between membrane module (7) and membrane bioreactor (8) sidewall guide shell (9) is set; Wherein form outlet system by water outlet-back flushing three-way solenoid valve (14), water outlet constant current suction pump (15), discharge pressure table (17), water flow meter (18) and filtered water tank (19), membrane module (7) water outlet links to each other with water outlet-back flushing three-way solenoid valve (14), water outlet-back flushing three-way solenoid valve (14) is gone up water-in by water outlet constant current suction pump (15) and filtered water tank (19) and is linked to each other, and the pipeline between water outlet constant current suction pump (15) and filtered water tank (19) is installed discharge pressure table (17) and water flow meter (18); Wherein form back-purge system by water outlet-back flushing three-way solenoid valve (14), backwashing pump (20), backwashing pressure table (22), back flushing under meter (23) and filtered water tank (19), water outlet-back flushing three-way solenoid valve (14) links to each other with filtered water tank (19) lower-left water outlet by backwashing pump (20), and the pipeline between backwashing pump (20) and water outlet-back flushing three-way solenoid valve (14) is installed backwashing pressure table (22) and back flushing under meter (23); Wherein by spoil disposal three-way solenoid valve (24), sludge pump (25), mud storage pool (26), spoil disposal liquid level sensor (27), mud valve (28) and filtered water tank (19) are formed sludge drainage system, mud storage pool (26) links to each other with the spoil disposal three-way solenoid valve by sludge pump (25), spoil disposal three-way solenoid valve (24) links to each other with filtered water tank (19) bottom right water outlet with membrane bioreactor (8) outlet at bottom respectively, a spoil disposal liquid level sensor (27) is installed in mud storage pool (26), spoil disposal liquid level sensor (27) has two probes, be respectively that mud stops probe (27-1) and clear water stops probe (27-2), at the pipeline of mud storage pool (26) mud discharging mouth a mud valve (28) be installed; Administration device (6) is installed in membrane bioreactor (8) top; Utilize the switch situation of programmable logic controller (29) control intake pump (2) and sludge pump (25), utilize programmable logic controller (29) by first frequency transformer (13), second frequency transformer (16) and the 3rd frequency transformer (21) are controlled pneumatic pump (12) respectively, switch and the running condition of water outlet constant current suction pump (15) and backwashing pump (20), inlet gage (3), flooding velocity meter (4), water inlet liquid level sensor (5), gas meter (11), discharge pressure table (17), water flow meter (18), backwashing pressure table (22), the information that back flushing under meter (23) and spoil disposal liquid level sensor (27) show feeds back to upper computer (30) by programmable logic controller (29), demonstrates inlet gage (3) at upper computer (30), flooding velocity meter (4), water inlet liquid level sensor (5), gas meter (11), discharge pressure table (17), water flow meter (18), backwashing pressure table (22), the actual information of back flushing under meter (23) and spoil disposal liquid level sensor (27).
2. utilize the method for the high ammonia nitrogen source water of the described a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay of claim 1, the method that it is characterized in that the high ammonia nitrogen source water of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay is to finish according to the following steps: one, start: at first high ammonia nitrogen source water adds in distribution reservoir (1) and the membrane bioreactor (8) with the low-temperature and low turbidity high luminance relay to be 3 ℃～5 ℃ in temperature, the liquid level of the high ammonia nitrogen source water of pending low-temperature and low turbidity high luminance relay is between upper limit water-level probe (5-1) sound end and lower limit water-level probe (5-2) sound end in the membrane bioreactor (8), water inlet liquid level sensor (5) is given programmable logic controller (29) with signal feedback, programmable logic controller this moment (29) control administration device (6) starts, the modified paligorskite sorbent material that flocculates is added in the membrane bioreactor (8), dosage is 30g/L～40g/L, programmable logic controller (29) starts pneumatic pump (12) by control first frequency transformer (13) simultaneously, making aeration tube (10) is that 480L/h～640L/h carries out aeration with the aeration rate, aeration rate shows by gas meter (11), data feed back to programmable logic controller (29), and show at upper computer (30), when if gas meter (11) shows that at upper computer (30) numerical value is lower than 480L/h or is higher than 640L/h, programmable logic controller (29) is regulated to the instruction of first frequency transformer (13) output operating frequency, the rotating speed of control pneumatic pump (12), till with the aeration rate being 480L/h～640L/h to aeration tube (10), combined type automatic control this moment membrane bioreactor starts to be finished; Two, fully automatic operation: after the startup of combined type automatic control membrane bioreactor is finished, by upper computer (30) editor water inlet system, the membrane bioreactor water treatment system, outlet system, back-purge system, the running condition of sludge drainage system and administration device (6), then the program that edits is inputed to programmable logic controller (29), carry out the program that upper computer (30) edits by programmable logic controller (29), namely utilize the switch situation of programmable logic controller (29) control intake pump (2) and sludge pump (25), utilize programmable logic controller (29) by first frequency transformer (13), second frequency transformer (16) and the 3rd frequency transformer (21) are controlled pneumatic pump (12) respectively, switch and the running condition of water outlet constant current suction pump (15) and backwashing pump (20), combined type automatic control membrane bioreactor are normally moved the back can collect clear water after obtaining handling at filtered water tank (19).
3. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 2, it is characterized in that the flocculation of modified paligorskite described in step 1 sorbent material specifically prepares according to the following steps: one, purify: at first natural polygorskite and deionized water are by mass ratio 1: (18～99) are added to natural polygorskite in the deionized water, low whipping speed is dispersed with stirring 10min～30min under 1000r/min～10000r/min then, obtain clay slip, again clay slip is placed whizzer, and be centrifugation 10min～20min under 4000r/min～12000r/min at centrifugal rotational speed, obtain the canescence clay puddle through separation, and be to dry to constant weight under 80 ℃～120 ℃ in temperature, after pulverizing 200 mesh sieves again, namely obtaining particle diameter is polygorskite behind the following purifying of 200 orders; Two, load: at first be that to be dissolved in volume fraction be in 2% the glacial acetic acid for 85%～95% chitosan with deacetylation, and it is 20 ℃～100 ℃ in temperature, mixing speed is to be stirred to dissolving fully under 200r/min～400r/min, be that to add particle diameter be polygorskite behind the purifying below 200 orders for 10g/min～50g/min with the speed of adding then, and it is 20 ℃～100 ℃ in temperature, mixing speed is to continue to stir 2h～4h under 200r/min～400r/min, obtain suspension, employing concentration is that the NaOH of 0.5mol/L～1.5mol/L transfers to neutrality with suspension, be centrifugation 10min～20min under 4000r/min～12000r/min at centrifugal rotational speed then, and the solid that centrifugation is obtained adopts deionized water wash 4～6 times, solid after will washing then is 60 ℃～110 ℃ oven dry 12h～24h in temperature, after pulverizing 200 mesh sieves again, namely obtain modified paligorskite flocculation sorbent material; Deacetylation described in the step 2 is that 85%～95% chitosan mass and volume fraction are that the ratio of 2% glacial acetic acid volume is 1g: (30mL～120mL); The mass ratio that adds particle diameter described in the step 2 and be polygorskite and deacetylation behind the following purifying of 200 orders and be 85%～95% chitosan is (5～20): 1.
4. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 3, it is characterized in that upper computer described in the step 2 (30) editor water inlet system running condition, specifying information is as follows: when liquid level in the membrane bioreactor (8) is lower than lower limit water-level probe (5-2) sound end of water liquid level sensor (5) into, water inlet liquid level sensor (5) is given programmable logic controller (29) with message feedback, programmable logic controller (29) control intake pump (2) is opened, intake pump (2) is with in the high ammonia nitrogen source water of the low-temperature and low turbidity high luminance relay suction membrane bioreactor (8) in the distribution reservoir (1), when liquid level in the membrane bioreactor (8) touches upper limit water-level probe (5-1) sound end of water liquid level sensor (5) into, water inlet liquid level sensor (5) is given programmable logic controller (29) with message feedback, programmable logic controller (29) control intake pump (2) is closed, when if distribution reservoir (1) amount of the reserve water is not enough, when being inlet gage (3) with the numerical value of flooding velocity meter (4) indication much smaller than regime values, this message feedback is given programmable logic controller (29), and present at upper computer (30), the inlet gage (3) that presents when upper computer (30) and flooding velocity meter (4) indication numerical value are during much smaller than regime values, upper computer (30) shows alarm, if in time handle, the interior liquid level of membrane bioreactor (8) is lower than when into the lowest water level of water liquid level sensor (5) is popped one's head in (5-3) sound end, water inlet liquid level sensor (5) is given programmable logic controller (29) with message feedback, present grave warning at upper computer (30), all operational systems of programmable logic controller this moment (29) control combined type automatic control membrane bioreactor are closed.
5. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 4, it is characterized in that upper computer described in the step 2 (30) editor membrane bioreactor water treatment system running condition, specifying information is as follows: remove upper computer (30) when grave warning occurring, need close sewage disposal system, otherwise membrane bioreactor water treatment system continuous service in combined type automatic control membrane bioreactor operational process, namely wherein by membrane module (7), membrane bioreactor (8), guide shell (9), aeration tube (10), gas meter (11) and pneumatic pump (12) component film bio-reactor water treatment system, be that pneumatic pump (12) remains opened condition, it is that 480L/h～640L/h carries out aeration that aeration tube (10) is continued with the aeration rate.
6. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 5, it is characterized in that upper computer described in the step 2 (30) edits out water system running condition, specifying information is as follows: when the time is set to time of pumping, programmable logic controller (29) control water outlet-back flushing three-way solenoid valve (14) is communicated with water outlet constant current suction pump (15), and control water outlet-back flushing three-way solenoid valve (14) disconnects with backwashing pump (20), programmable logic controller (29) is opened by second frequency transformer (16) control water outlet constant current suction pump (15) simultaneously, and programmable logic controller (29) cuts out by the 3rd frequency transformer (21) control backwashing pump (20), the clear water that filtration obtains from membrane module (7) water outlet through water outlet-back flushing three-way solenoid valve (14), water outlet constant current suction pump (15) enters in the filtered water tank (19) with filtered water tank (19) water-in, the single time of pumping is 40min～60min, and membrane flux is 150L/m 2H～250L/m 2H is if water flow meter (18) shows that at upper computer (30) numerical value is lower than 150L/m 2H or be higher than 250L/m 2During h, programmable logic controller (29) is regulated to the instruction of second frequency transformer (16) output operating frequency, the rotating speed of control water outlet constant current suction pump (15), to membrane flux be 150L/m 2H～250L/m 2Till the h.
7. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 6, it is characterized in that upper computer described in the step 2 (30) editor back-purge system running condition, specifying information is as follows: when the time is set to backwashing time, programmable logic controller (29) control water outlet-back flushing three-way solenoid valve (14) is communicated with backwashing pump (20), and control water outlet-back flushing three-way solenoid valve (14) disconnects with water outlet constant current suction pump (15), programmable logic controller (29) is opened by the 3rd frequency transformer (21) control backwashing pump (20) simultaneously, and programmable logic controller (29) cuts out by the 3rd frequency transformer (16) control water outlet constant current suction pump (15), with back flushing water yield 1.05m 3/ m 2H～1.4m 3/ m 2H extracts the clear water in the filtered water tank (19) out from filtered water tank (19) lower-left water outlet, membrane module (7) is carried out back flushing, and the single backwashing time is 60s～120s, if back flushing under meter (23) shows that at upper computer (30) numerical value is lower than 1.05m 3/ m 2H or be higher than 1.4m 3/ m 2During h, programmable logic controller (29) is regulated to the instruction of second frequency transformer (21) output operating frequency, and the rotating speed of control backwashing pump (20) is to back flushing water yield 1.05m 3/ m 2H～1.4m 3/ m 2Till the h; Programmable logic controller (29) setting is water outlet-backwashing period with a water outlet time and a backwashing time sum, back and forth start outlet system and back-purge system in the operational process, back flushing next time began when namely a time of pumping finished, and one time backwashing time finishes the while beginning of drawing water next time.
8. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 7, it is characterized in that upper computer described in the step 2 (30) editor sludge drainage system running condition, specifying information is as follows: combined type automatic control membrane bioreactor will regularly carry out spoil disposal in operational process, combined type automatic control membrane bioreactor is set, and spoil disposal is once when operation 2000～3000 water outlets-backwashing period, namely after finishing, the backwashing time of operation 2000～3000 water outlets-backwashing period enters the spoil disposal time, and this moment, outlet system was out of service, and outlet system continues operation again after the spoil disposal time finishes; Be set to spoil disposal during the time when the time, programmable logic controller (29) control spoil disposal three-way solenoid valve (24) is communicated with membrane bioreactor (8) bottom mud discharging mouth, and spoil disposal three-way solenoid valve (24) disconnects with clean water basin (19) bottom right water outlet, mud drains in the mud storage pool (26) through spoil disposal three-way solenoid valve (24) and sludge pump (25), when the mud face touches mud termination probe (27-1) sound end of spoil disposal liquid level sensor (27), spoil disposal liquid level sensor (27) with signal feedback to programmable logic controller (29), programmable logic controller (29) control spoil disposal three-way solenoid valve (24) disconnects with membrane bioreactor (8) bottom mud discharging mouth, and be connected with filtered water tank (19) bottom right water outlet, the clear water of filtered water tank (19) is through spoil disposal three-way solenoid valve (24), sludge pump (25) drains in the mud storage pool (26), when the mud face touches clear water termination probe (27-2) sound end of spoil disposal liquid level sensor (27), spoil disposal liquid level sensor (27) with signal feedback to programmable logic controller (29), programmable logic controller (29) control spoil disposal three-way solenoid valve (24) is all closed with sludge pump (25), and the sludge drainage system operation is once finished.
9. the method for the high ammonia nitrogen source water of a kind of combined type automatic control Membrane Bioreactor for Wastewater Treatment low-temperature and low turbidity high luminance relay according to claim 2, it is characterized in that upper computer described in the step 2 (30) editor administration device (6) running condition, specifying information is as follows: when the mud face touches clear water termination probe (27-2) sound end of spoil disposal liquid level sensor (27), spoil disposal liquid level sensor (27) with signal feedback to programmable logic controller (29), programmable logic controller (29) control administration device (6) adds the modified paligorskite sorbent material that flocculates in the membrane bioreactor (8), when dosage when being 6g/L～10g/L programmable logic controller (29) control administration devices (6) close.
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