CN110950434A - MBR sewage treatment system and control method thereof - Google Patents
MBR sewage treatment system and control method thereof Download PDFInfo
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- CN110950434A CN110950434A CN201911149276.5A CN201911149276A CN110950434A CN 110950434 A CN110950434 A CN 110950434A CN 201911149276 A CN201911149276 A CN 201911149276A CN 110950434 A CN110950434 A CN 110950434A
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- 239000010865 sewage Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000012528 membrane Substances 0.000 claims abstract description 181
- 238000005273 aeration Methods 0.000 claims abstract description 125
- 239000010802 sludge Substances 0.000 claims abstract description 32
- 206010021143 Hypoxia Diseases 0.000 claims abstract description 22
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 37
- 239000007789 gas Substances 0.000 claims description 21
- 239000000945 filler Substances 0.000 claims description 17
- 230000001105 regulatory effect Effects 0.000 claims description 13
- 210000004177 elastic tissue Anatomy 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims 1
- 230000001276 controlling effect Effects 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 18
- 238000004140 cleaning Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 230000000694 effects Effects 0.000 abstract description 11
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 9
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 9
- 239000011574 phosphorus Substances 0.000 abstract description 9
- 230000001965 increasing effect Effects 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 5
- 230000009471 action Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000011010 flushing procedure Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000001934 delay Effects 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000009991 scouring Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000000338 in vitro Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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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
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to the technical field of sewage treatment, and provides an MBR sewage treatment system and a control method thereof. Including oxygen deficiency pond, anaerobism pond and the good oxygen pond of intercommunication in order, good oxygen pond still communicates there are a plurality of membrane cisterns, and is a plurality of the membrane cisterns with oxygen deficiency pond intercommunication still includes the membrane module, the membrane module is equallyd divide for the multiunit to correspond to arrange in a plurality of in the membrane cisterns, the multiunit the membrane module is connected with membrane module aeration equipment respectively, the multiunit the membrane module aeration equipment passes through the flow divider valve and is connected with the air supply. All the air quantity is supplied to a group of membrane module aeration devices in turn through a flow divider valve, so that the aeration quantity is relatively increased without increasing energy consumption to enhance the cleaning effect of the membrane module; the activated sludge can be continuously converted in aerobic, anoxic and anaerobic environments, thereby achieving the purpose of deep nitrogen and phosphorus removal.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to an MBR sewage treatment system and a control method thereof.
Background
MBR (Membrane bioreactor) is a sewage treatment process combining Membrane separation technology with a traditional biological treatment unit. In the operation process, the membrane material has a certain service life and needs to be replaced periodically; meanwhile, in order to maintain the normal operation of the conventional MBR, a continuous high-strength aeration method is adopted to maintain the high scouring cross-flow speed of the membrane surface to delay membrane pollution. The conventional MBR mostly adopts perforated pipe aeration, and the effective utilization rate of the aeration energy consumption of membrane surface scouring is less than 30 percent, so that the aeration energy consumption is huge, but the utilization rate is not high; meanwhile, strict aerobic in the reaction tank is caused by huge aeration amount in the MBR tank, and anaerobic/anoxic and aerobic hydraulic circulation conditions necessary for nitrogen and phosphorus removal cannot be formed, so that the nitrogen and phosphorus removal efficiency is very low and is close to zero.
The variable aeration is that the membrane modules are divided into two groups and then are respectively connected with an air supply pipe of an air source through an electric valve, and in the operation process, one electric valve is closed in turn to concentrate all air quantity on one group of membrane modules, so that the membrane modules obtain scrubbing aeration quantity which is several times of that of the membrane modules within a certain time to better delay membrane pollution, and the total aeration quantity is unchanged.
In the actual operation process, the integrated MBR equipment with low consumption is formed by partitioning the reaction tank through the partition plates and is divided into a membrane tank, an anoxic tank and an anaerobic tank which are arranged outside the membrane tank. Under the normal condition, under the aeration action, the mixed sludge in the membrane tank flows out of the membrane tank due to larger aeration quantity, namely flows to the anoxic tank and the anaerobic tank, the activated sludge naturally experiences an anoxic anaerobic environment, and the nitrogen and phosphorus removal effect is better. After variable aeration is adopted, one group of membrane group obtains several times scrubbing aeration amount in the membrane pool under the variable aeration state, the other group of membrane group is in a state that the aeration amount is very low or even zero, the air amount in the membrane pool area is unbalanced, the mixed liquid in the high aeration area at the upper part in the membrane pool can flow to the low aeration area or the non-aeration area, the mixed sludge outside the membrane pool can flow back to the membrane pool, the flow state is unbalanced and the flow direction of the mixed sludge is changed, the anaerobic environment which is necessary for forming activated sludge is not facilitated, the denitrification and dephosphorization effects are influenced, and the removal effect of the total nitrogen and total phosphorus in the effluent is unstable.
Disclosure of Invention
The invention aims to provide an MBR sewage treatment system, which realizes deep denitrification and dephosphorization, reduces the aeration energy consumption of a membrane tank, improves the flushing effect of a membrane component and delays membrane pollution.
In order to achieve the purpose, the invention adopts the following technical scheme: the utility model provides a MBR sewage treatment system, is including oxygen deficiency pond, anaerobism pond and the good oxygen pond of intercommunication in order, good oxygen pond still communicates has a plurality of membrane cisternas, and is a plurality of the membrane cisterna with oxygen deficiency pond intercommunication still includes the membrane module, the membrane module is equallyd divide for the multiunit to correspond to arrange in a plurality of in the membrane cisterna, the multiunit the membrane module is connected with membrane module aeration equipment separately, the multiunit the membrane module aeration equipment passes through the flow divider valve and is connected with the air supply.
Optionally, the membrane cisterna is provided with two, the oxygen deficiency pond sets up in two between the membrane cisterna, two the bottom in membrane cisterna communicates and the same diapire of sharing each other, the diapire in oxygen deficiency pond and two the diapire interval of membrane cisterna arranges, be provided with in the oxygen deficiency pond by the air stripping device of air supply air feed, the air stripping device passes the diapire in oxygen deficiency pond and two the bottom intercommunication in membrane cisterna.
Optionally, the lower part of oxygen deficiency pond be funnel type and the lower part with the anaerobism pond intercommunication, the air stripping device includes coaxial inside and outside air supply pipe and the air stripping pipe of arranging, the water inlet of air stripping pipe is big horn shape about the size, the delivery port of air stripping pipe is in the upper portion of oxygen deficiency pond, the air inlet of air supply pipe with the air supply is connected.
Optionally, a plurality of membrane tanks are also provided with aeration gas collecting devices.
Optionally, the plurality of groups of membrane modules are respectively connected with the suction pump through a water collecting main pipe.
Optionally, the gas source is correspondingly connected with the perforated aeration pipe in the anaerobic tank and the microporous aeration pipe in the aerobic tank through the anaerobic tank aeration main pipe and the aerobic tank aeration main pipe.
Optionally, the anoxic tank and the anaerobic tank are correspondingly connected with the water inlet main pipe through an anoxic tank water inlet regulating valve and an anaerobic tank water inlet regulating valve.
Optionally, a filler support is arranged in the anaerobic tank, and a braided filler or an elastic fiber filler or a composite filler is suspended on the filler support.
The invention also aims to provide a control method of the MBR sewage treatment system, which realizes deep denitrification and dephosphorization, reduces the aeration energy consumption of the membrane tank, improves the flushing effect of the membrane module and delays membrane pollution.
In order to achieve the purpose, the invention adopts the following technical scheme: a control method of an MBR sewage treatment system comprises the following steps:
A. supplying activated sludge to the anoxic tank, the anaerobic tank or the aerobic tank, and supplying sewage to the anoxic tank or the anaerobic tank;
B. when the system runs stably, the circulation flow of the activated sludge is as follows: an aerobic tank, a plurality of membrane tanks, an anoxic tank, an anaerobic tank and an aerobic tank;
C. the number of membrane tanks is set as n (n)>1) Setting the aeration rate of the membrane component aeration device of each membrane tank as Xm3The total aeration rate of the air source to the membrane tank is nXm3Intermittent making m (1 ≦ m) through the flow dividing valve during the system operation<The membrane component aeration devices of the n) membrane tanks stop working, and the aeration quantity of the membrane component aeration devices of the rest n-m membrane tanks is changed into nX/(n-m) m3/h。
The number of the membrane tanks is two, the anoxic tank is arranged between the two membrane tanks, and the bottoms of the two membrane tanks are mutually communicated and share the same bottom wall;
the suction pump is opposite to the membrane tank through the water collecting main pipeIntermittently pumping water, wherein the conventional aeration rate of the two membrane component aeration devices is Xm during the starting period of the suction pump3When the suction pump is closed, the two membrane component aeration devices are alternatively closed through the flow dividing valve, and the aeration rate of the membrane component aeration device which is not closed is 2Xm3/h。
Compared with the prior art, the method has the following technical effects:
(1) low energy consumption
Adopts variable aeration, and the energy consumption is only conventional MBR technology (0.8-0.9 kWh/m)3) 40-50% of the total amount of the active carbon, and reaches the international advanced level (0.4-0.5 kWh/m) of the energy consumption of the technology3)；
(2) Small land occupation and good effluent quality
Compared with the traditional activated sludge method, the method reduces the floor area of the equipment by more than 50 percent, and saves the floor area by 10 to 15 percent compared with the conventional MBR equipment; the effluent quality stably reaches the first-class A standard GB18918-2002 discharge Standard of pollutants for municipal wastewater treatment plants;
(3) simple and convenient operation
The membrane pollution development becomes slow, the membrane cleaning frequency is low (1 time of on-line cleaning in half a year), and the labor intensity is low. The operation is simple and convenient; the automation degree is high, and unattended operation can be realized;
(4) high adaptability
The modular sewage treatment system is more suitable for various sewage treatment projects such as large, medium and small sewage treatment projects due to the unitized, modular and standardized design, and is convenient for rapid popularization in large, medium and small towns and rural areas;
(5) low construction cost and low operating cost
In a word, this application MBR sewage treatment system has possessed low energy consumption, high nitrogen and phosphorus removal efficiency, goes out that water quality of water is good, takes up an area of for a short time, convenient operation, shock load resistance strong characteristics. The modular, modularized and standardized design of the membrane module makes the membrane module more suitable for various sewage treatment scales, and greatly shortens the production period and the engineering period of equipment.
Drawings
FIG. 1 is a top view of the present invention;
FIG. 2 is a cross-sectional view taken along line A-A of FIG. 1;
FIG. 3 is a cross-sectional view taken along line B-B of FIG. 1;
FIG. 4 is a cross-sectional view taken along line C-C of FIG. 1;
fig. 5 is a cross-sectional view taken along line D-D of fig. 1.
Reference numerals:
1. an anoxic tank; 2. an anaerobic tank; 3. an aerobic tank; 4. a membrane tank; 5. a membrane module; 6. a membrane module aeration device; 7. a flow divider valve; 8. a gas source; 9. a gas stripping device; 91. a gas supply pipe; 92. a gas stripping tube; 10. a water collecting main pipe; 11. a suction pump; 12. an aeration main pipe of the anaerobic tank; 13. an aeration main pipe of the aerobic tank; 14. perforating an aeration pipe; 15. a microporous aeration pipe; 16. the water inlet regulating valve of the anoxic tank; 17. the water inlet regulating valve of the anaerobic tank; 18. a water inlet main pipe; 19. a filler support; 20. aeration gas-collecting device.
Detailed Description
In order that the above objects, features and advantages of the present invention can be more clearly understood, the present invention will be further described in detail with reference to the accompanying drawings and examples. It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. The specific embodiments described herein are merely illustrative of the invention and are not to be construed as limiting the invention. All other embodiments, which can be derived by a person skilled in the art from the described embodiments of the invention, are within the scope of the invention.
As shown in fig. 1, the MBR sewage treatment system provided by the invention comprises an anoxic tank 1, an anaerobic tank 2 and an aerobic tank 3 which are sequentially communicated, wherein the aerobic tank 3 is also communicated with a plurality of membrane tanks 4, the membrane tanks 4 are communicated with the anoxic tank 1, the MBR sewage treatment system further comprises membrane components 5, the membrane components 5 are uniformly distributed in the membrane tanks 4 in a plurality of groups, the membrane components 5 are respectively connected with membrane component aeration devices 6, and the membrane component aeration devices 6 are connected with an air source 8 through a shunt valve 7.
Compared with the prior art, the aerobic tank 3 and the membrane tanks 4 are arranged behind the anoxic tank 1 and the anaerobic tank 2, variable aeration can be realized by a plurality of sets of membrane component aeration devices 6 in the membrane tanks 4 through the diverter valve 7, namely all air flow is intensively supplied to one set of membrane component aeration devices 6 through the diverter valve 7 in turn, so that the aeration quantity is relatively increased without increasing energy consumption to enhance the cleaning effect of the membrane component 5, and the membrane tanks 4 are mutually separated, so that the condition that a high aeration quantity area flows to a low aeration area or a non-aeration area can not occur, and the condition of turbulence does not exist among the membrane tanks 4, therefore, the mixed liquid in the membrane tanks 4 can not flow back to the aerobic tank 3, even though the mixed liquid flows back, a small part of the mixed liquid flows back to the aerobic tank 3, wherein the mixed liquid rich in oxygen is the aerobic environment required by the aerobic tank 3, and the mixed liquid can not flow back to the anaerobic tank 2 to influence the anaerobic environment thereof, the activated sludge in the membrane tanks 4 is timely conveyed into the anoxic tank 1, the activated sludge forms a circulation of 'aerobic tank 3-a plurality of membrane tanks 4-anoxic tank 1-anaerobic tank 2-aerobic tank 3', and the activated sludge can be continuously converted in aerobic, anoxic and anaerobic environments, so that the aim of deep nitrogen and phosphorus removal is fulfilled.
In some embodiments, two membrane tanks 4 may be provided, and if too many membrane tanks 4 are provided, when one of the membrane tanks 4 is intensively aerated in turn, the time interval for waiting for the intensive aeration of the other membrane tank 4 will increase, which will not be beneficial to cleaning the membrane module 5; ingenious utilization oxygen deficiency pond 1 separates two membrane cisternas 4, the bottom of two membrane cisternas 4 still has a intercommunication region, this intercommunication region is used for letting air stripping device 9 with the one-way transport of the activated sludge mixed liquid in two membrane cisternas 4 to oxygen deficiency pond 1, when concentrating the aeration in turn, the intercommunication region still has the condition that probably has the vortex, but the shared volume in intercommunication region is little, air stripping device 9 also can in time carry the activated sludge mixed liquid in this region to oxygen deficiency pond 1 in, so the influence that the vortex condition caused can be ignored, and this application adopts air stripping device 9 and membrane module aeration device 6 sharing air supply 8, need not additionally arrange elevator pump or motor etc. the effectual device that has simplified arranges, the cost is saved.
In some embodiments, the lower part of the anoxic pond 1 is funnel-shaped and the lower part is communicated with the anaerobic pond 2, the gas stripping device 9 comprises a gas supply pipe 91 and a gas stripping pipe 92 which are coaxially arranged inside and outside, the water inlet of the gas stripping pipe 92 is in a shape of a horn with a small upper part and a large lower part, the water outlet of the gas stripping pipe 92 is positioned at the upper part of the anoxic pond 1, and the gas inlet of the gas supply pipe 91 is connected with the gas source 8. The large air-lift circulation power generated by the high-strength aeration of the air-lift device 9 enables the activated sludge mixed liquor to flow to the upper part of the anoxic tank 1 from the bottoms of the two membrane tanks 4 in a one-way mode through the air-lift pipe 92, then the activated sludge mixed liquor generates anoxic reaction from top to bottom and then automatically flows to the anaerobic tank 2, and then returns to the membrane tank 4 through the aerobic tank 3 to form activated sludge biological reaction circulation.
In some embodiments, an aeration gas collecting device 20 is further arranged in the plurality of membrane tanks 4. The aeration gas collecting device 20 is used for collecting waste gas generated in the membrane tank 4 and surplus gas generated when the membrane component aeration device 6 washes the membrane component 5, and the dissolved oxygen concentration of the anoxic tank 1 is not too high, so that the timely collection of the gas in the membrane tank 4 is beneficial to reducing the dissolved oxygen concentration of the activated sludge mixed liquid flowing to the anoxic tank 1.
In some embodiments, the plurality of membrane modules 5 are each connected to a suction pump 11 via a collection header 10, the suction pump 11 operating to collect purified water.
In some embodiments, the air source 8 is connected to the perforated aeration pipe 14 in the anaerobic tank 2 and the microporous aeration pipe 15 in the aerobic tank 3 through the anaerobic tank aeration main pipe 12 and the aerobic tank aeration main pipe 13, respectively. The anaerobic tank 2 is aerated intermittently through the perforated aeration pipe 14, sludge in the anaerobic tank 2 can be uniformly mixed to flow, anaerobic reaction is favorably generated, the aerobic tank 3 is aerated through the microporous aeration pipe 15, the dissolved oxygen concentration of the aerobic tank 3 is ensured, and the aerobic reaction is favorably generated.
In some embodiments, the anoxic tank 1 and the anaerobic tank 2 are connected with the water inlet manifold 18 through an anoxic tank inlet regulating valve 16 and an anaerobic tank inlet regulating valve 17, and the water quantity is regulated through the anoxic tank inlet regulating valve 16 and the anaerobic tank inlet regulating valve 17.
In some embodiments, a filler support 19 is arranged in the anaerobic tank 2, and a braided filler or an elastic fiber filler or a composite filler is hung on the filler support 19. In the practical application process, the filler can be arranged in the anaerobic tank 2 or the anoxic tank 1, so that the aggregation growth of microorganisms is facilitated, and the nitrogen and phosphorus removal effect is improved.
A control method of an MBR sewage treatment system comprises the following steps:
A. activated sludge is supplied to the anoxic tank 1, the anaerobic tank 2 or the aerobic tank 3, and sewage is supplied to the anoxic tank 1 or the anaerobic tank 2;
B. when the system runs stably, the circulation flow of the activated sludge is as follows: an aerobic tank 3-a plurality of membrane tanks 4-an anoxic tank 1-an anaerobic tank 2-an aerobic tank 3;
C. the number of the membrane tanks 4 is set as n (n)>1) Setting the aeration rate of the membrane component aeration device 6 of each membrane tank 4 as Xm3H, the total aeration rate of the air source 8 to the membrane tank 4 is nXm3H, intermittently making m (1. ltoreq. m) by the flow dividing valve 7 during the operation of the system<The membrane component aeration devices 6 of the n) membrane tanks 4 stop working, and the aeration quantity of the membrane component aeration devices 6 of the rest n-m membrane tanks 4 is changed into nX/(n-m) m3/h。
Compared with the prior art, the variable aeration method can intermittently improve the aeration quantity of the membrane component aeration device 6 on the premise of not increasing the energy consumption, thereby enhancing the washing effect of the membrane component 5, further delaying the membrane pollution, and correspondingly reducing the cost of cleaning the membrane or replacing the membrane; the activated sludge in the membrane tanks 4 is timely conveyed into the anoxic tank 1, the activated sludge forms a circulation of 'aerobic tank 3-a plurality of membrane tanks 4-anoxic tank 1-anaerobic tank 2-aerobic tank 3', and the activated sludge can be continuously converted in aerobic, anaerobic and anoxic environments, so that the aim of deep nitrogen and phosphorus removal is fulfilled.
The suction pump 11 pumps the membrane tank 4 intermittently through the water collecting main pipe 10, and the conventional aeration rate of the two membrane component aeration devices 6 is Xm during the starting period of the suction pump 113When the suction pump 11 is closed, the two membrane component aeration devices 6 are alternatively closed through the flow dividing valve 7, and the aeration rate of the membrane component aeration device 6 which is not closed is 2Xm3And h, the aeration flushing effect on the membrane modules 5 can be enhanced by alternately concentrating aeration while ensuring the conventional aeration amount by adopting the adjusting mode, and the aeration amount is twice of the conventional aeration amount, so that the dirt is prevented from being attached to the membrane modules 5 during the closing period of the suction pump 11.
The aeration rate of the two membrane component aeration devices 6 is X/2m3The aeration rate is half of the conventional aeration rate, the corresponding energy consumption is also reduced by half, the two membrane component aeration devices 6 are alternatively closed through the flow dividing valve 7 during the closing period of the suction pump 11, and the membrane component aeration device 6 which is not closed exposesThe gas amount is Xm3The Xm can be realized by adopting the alternative concentrated aeration mode while reducing the conventional power consumption by adopting the adjusting mode3Conventional aeration per hour.
The following are specific examples of the present invention:
the air supply of the air source 8 is divided into four paths, and one path is connected with the two groups of membrane component aeration devices 6 through the flow dividing valve 7; the other path is connected with a perforated aeration pipe 14 through an aeration main pipe 12 of the anaerobic tank; the third path passes through an aeration main pipe 13 of the aerobic tank and a microporous aeration pipe 15; the fourth path is connected to the gas supply pipe 91 via a regulating valve.
Debugging the MBR sewage treatment system: the tank body is filled with water to ensure that the tank body is not seeped or leaked. After the pool body has no problem, clear water is injected into the connecting pipeline of the suction pump 11, and the single-machine trial operation is carried out on the air source 8 and the suction pump 11, so that the pipelines and the joints of the pipelines and the equipment are ensured to be free from leakage. And (4) checking whether the four paths of air supply of the air source 8 are uniform and normal, or else, overhauling until the aeration system is qualified. The suction pump 11 is activated and the regulating valve is activated so that the pumping flow rate becomes equal to the set value.
The MBR sewage treatment system operates: activated sludge is added into the reaction tank, and sewage debugging is started. The control state is firstly set to be automatically operated, and the water outlet of the suction pump 11 can be debugged and operated according to the small flux of the full load 1/4-1/2; adjusting an anoxic tank water inlet adjusting valve 16 and an anaerobic tank water inlet adjusting valve 17 on a water inlet main pipe 18 to ensure that the water inflow distribution of the anoxic tank 1 and the anaerobic tank 2 meets the design requirement; simultaneously, adjusting the air supply of each path to ensure that the DO of the anoxic tank 1 is below 0.3mg/L and the DO of the anaerobic tank 2 is below 0.1mg/L, and ensuring that the anoxic tank 1 and the anaerobic tank 2 are respectively in anoxic and anaerobic environments; starting an automatic program, intermittently operating the suction pump 11, and setting the intermittent operation and the stop time to be 4-13min:1.5-2 min;
the membrane component aeration devices 6 in the two membrane tanks 2 alternately perform full closing and full opening actions once during the single closing period of the suction pump 11; or one of the membrane component aeration devices 6 is intensively aerated during the first closing period of the suction pump 11, the other membrane component aeration device 6 is intensively aerated during the second closing period of the suction pump 11, and the like, the two membrane component aeration devices 6 alternately perform the full closing and the full opening actions once during the two closing periods.
The reaction tank is provided with a high liquid level, a middle liquid level and a low liquid level, when the liquid level is in the middle, a lifting pump of the adjusting tank is started to supplement water to the reaction tank through the water inlet main pipe 18, and when the liquid level is in the high liquid level, the water supplement of the lifting pump is stopped; when the liquid level is low, the system stops running and gives an alarm, and when the sludge concentration rises to 6g/L, the system can be increased to run at full load; when the sludge concentration exceeds 9-12g/L, the sludge can be discharged periodically, and the sludge discharge amount is carried out according to the set sludge age.
Cleaning of the membrane module 5: the membrane detaching piece cleaning mode is operated as follows: 0.3 percent sodium hypochlorite solution is prepared in the chemical cleaning pool, the membrane is taken out and washed clean by clear water, and then is put into the chemical cleaning pool to be soaked for about 24 hours, so that the chemical cleaning of the membrane by external immersion can be completed.
Because the in vitro immersion cleaning operation can be carried out in batches, each batch can be limited to 1 group of membrane modules, the operation of other membrane modules of the equipment is not influenced, and the continuous operation requirement of the engineering can be met.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. The utility model provides a MBR sewage treatment system which characterized in that: including oxygen deficiency pond (1), anaerobism pond (2) and good oxygen pond (3) that communicate in order, good oxygen pond (3) still communicate has a plurality of membrane cisterns (4), and is a plurality of membrane cisterns (4) with oxygen deficiency pond (1) intercommunication still includes membrane module (5), membrane module (5) are equallyd divide for the multiunit to correspond to arrange in a plurality of in membrane cisterns (4), the multiunit membrane module (5) are connected with membrane module aeration equipment (6) respectively, the multiunit membrane module aeration equipment (6) are connected with air supply (8) through flow divider valve (7).
2. The MBR sewage treatment system of claim 1, wherein: the utility model discloses a membrane pond, including membrane pond (4), oxygen deficiency pond (1) and air source (8), membrane pond (4) are provided with two, oxygen deficiency pond (1) sets up in two between membrane pond (4), two the bottom of membrane pond (4) communicates each other and the same diapire of sharing, the diapire and two of oxygen deficiency pond (1) the diapire interval of membrane pond (4) is arranged, be provided with in oxygen deficiency pond (1) by air stripping device (9) of air supply (8) air feed, air stripping device (9) are passed the diapire and two of oxygen deficiency pond (1) the bottom intercommunication of membrane pond (4).
3. The MBR sewage treatment system of claim 2, wherein: the lower part of oxygen deficiency pond (1) be funnel type and lower part with anaerobism pond (2) intercommunication, air stripping device (9) are including coaxial inside and outside air supply pipe (91) and the air stripping pipe (92) of arranging, the water inlet of air stripping pipe (92) is big horn shape about the small, the delivery port of air stripping pipe (92) is in the upper portion of oxygen deficiency pond (1), the air inlet of air supply pipe (91) with air supply (8) are connected.
4. The MBR sewage treatment system of claim 1, wherein: and aeration gas collecting devices (20) are also arranged in the membrane tanks (4).
5. The MBR sewage treatment system of claim 1, wherein: the membrane modules (5) are respectively connected with a suction pump (11) through a water collecting main pipe (10).
6. The MBR sewage treatment system of claim 1, wherein: the air source (8) is correspondingly connected with a perforated aeration pipe (14) in the anaerobic tank (2) and a microporous aeration pipe (15) in the aerobic tank (3) through an anaerobic tank aeration main pipe (12) and an aerobic tank aeration main pipe (13).
7. The MBR sewage treatment system of claim 1, wherein: the anoxic tank (1) and the anaerobic tank (2) are correspondingly connected with a water inlet main pipe (18) through an anoxic tank water inlet regulating valve (16) and an anaerobic tank water inlet regulating valve (17).
8. The MBR sewage treatment system of claim 1, wherein: be provided with filler support (19) in anaerobism pond (2), hang pigtail formula filler or elastic fiber filler or compound filler on filler support (19).
9. A control method of an MBR sewage treatment system is characterized in that: the method comprises the following steps:
A. activated sludge is supplied to the anoxic tank (1), the anaerobic tank (2) or the aerobic tank (3), and sewage is supplied to the anoxic tank (1) or the anaerobic tank (2);
B. when the system runs stably, the circulation flow of the activated sludge is as follows: an aerobic tank (3), a plurality of membrane tanks (4), an anoxic tank (1), an anaerobic tank (2) and an aerobic tank (3);
C. the number of the membrane tanks (4) is set as n (n)>1) Setting the aeration rate of the membrane component aeration device (6) of each membrane pool (4) as Xm3H, the total aeration rate of the air source (8) to the membrane tank (4) is nXm3H, intermittently making m (1 ≦ m) by the diverter valve (7) during system operation<The membrane component aeration devices (6) of the n membrane tanks (4) stop working, and the aeration quantity of the membrane component aeration devices (6) of the rest n-m membrane tanks (4) is changed into nX/(n-m) m3/h。
10. The method of controlling an MBR sewage treatment system of claim 9, wherein: the number of the membrane tanks (4) is two, the anoxic tank (1) is arranged between the two membrane tanks (4), and the bottoms of the two membrane tanks (4) are mutually communicated and share the same bottom wall;
the suction pump (11) pumps water intermittently from the membrane tank (4) through the water collecting main pipe (10), and the conventional aeration rate of the two membrane component aeration devices (6) is Xm during the starting period of the suction pump (11)3H, during the closing period of the suction pump (11), the two membrane component aeration devices (6) are closed alternately through the flow dividing valve (7), and the aeration quantity of the membrane component aeration device (6) which is not closed is 2Xm3/h。
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