CN112591876A - Offline recovery cleaning method of distributed sewage treatment MBR system - Google Patents
Offline recovery cleaning method of distributed sewage treatment MBR system Download PDFInfo
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- 238000004140 cleaning Methods 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000010865 sewage Substances 0.000 title claims abstract description 33
- 238000011084 recovery Methods 0.000 title description 15
- 239000012528 membrane Substances 0.000 claims abstract description 139
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 123
- 239000007788 liquid Substances 0.000 claims abstract description 71
- 238000010992 reflux Methods 0.000 claims abstract description 66
- 238000005406 washing Methods 0.000 claims abstract description 52
- 239000010802 sludge Substances 0.000 claims abstract description 49
- 239000002699 waste material Substances 0.000 claims abstract description 30
- 238000002791 soaking Methods 0.000 claims abstract description 27
- 238000005554 pickling Methods 0.000 claims abstract description 26
- 238000007599 discharging Methods 0.000 claims abstract description 13
- 230000008569 process Effects 0.000 claims abstract description 10
- 239000006260 foam Substances 0.000 claims abstract description 9
- 230000029087 digestion Effects 0.000 claims abstract description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 30
- 239000002253 acid Substances 0.000 claims description 27
- 239000003513 alkali Substances 0.000 claims description 27
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 27
- 239000002738 chelating agent Substances 0.000 claims description 16
- 239000004094 surface-active agent Substances 0.000 claims description 16
- 239000012459 cleaning agent Substances 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 13
- 230000003068 static effect Effects 0.000 claims description 12
- 229940051841 polyoxyethylene ether Drugs 0.000 claims description 11
- 229920000056 polyoxyethylene ether Polymers 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 9
- 238000005260 corrosion Methods 0.000 claims description 9
- 230000007797 corrosion Effects 0.000 claims description 9
- 239000003112 inhibitor Substances 0.000 claims description 9
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 9
- LNOPIUAQISRISI-UHFFFAOYSA-N n'-hydroxy-2-propan-2-ylsulfonylethanimidamide Chemical compound CC(C)S(=O)(=O)CC(N)=NO LNOPIUAQISRISI-UHFFFAOYSA-N 0.000 claims description 8
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 7
- 239000000460 chlorine Substances 0.000 claims description 7
- 229910052801 chlorine Inorganic materials 0.000 claims description 7
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 6
- IGFHQQFPSIBGKE-UHFFFAOYSA-N Nonylphenol Natural products CCCCCCCCCC1=CC=C(O)C=C1 IGFHQQFPSIBGKE-UHFFFAOYSA-N 0.000 claims description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- SNQQPOLDUKLAAF-UHFFFAOYSA-N nonylphenol Chemical compound CCCCCCCCCC1=CC=CC=C1O SNQQPOLDUKLAAF-UHFFFAOYSA-N 0.000 claims description 6
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 4
- 229960001484 edetic acid Drugs 0.000 claims description 4
- 150000002191 fatty alcohols Chemical class 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 230000001131 transforming effect Effects 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000003599 detergent Substances 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 3
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 claims description 3
- 235000019982 sodium hexametaphosphate Nutrition 0.000 claims description 3
- 235000019832 sodium triphosphate Nutrition 0.000 claims description 3
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 claims description 3
- 239000003109 Disodium ethylene diamine tetraacetate Substances 0.000 claims description 2
- 150000001412 amines Chemical class 0.000 claims description 2
- 235000019301 disodium ethylene diamine tetraacetate Nutrition 0.000 claims description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 2
- UEUXEKPTXMALOB-UHFFFAOYSA-J tetrasodium;2-[2-[bis(carboxylatomethyl)amino]ethyl-(carboxylatomethyl)amino]acetate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-]C(=O)CN(CC([O-])=O)CCN(CC([O-])=O)CC([O-])=O UEUXEKPTXMALOB-UHFFFAOYSA-J 0.000 claims description 2
- 150000003585 thioureas Chemical class 0.000 claims description 2
- 230000001681 protective effect Effects 0.000 claims 1
- 230000004907 flux Effects 0.000 description 6
- 238000011065 in-situ storage Methods 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 5
- 229910052698 phosphorus Inorganic materials 0.000 description 5
- 239000011574 phosphorus Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005303 weighing Methods 0.000 description 4
- 239000003638 chemical reducing agent Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 238000011066 ex-situ storage Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- UMGDCJDMYOKAJW-UHFFFAOYSA-N thiourea Chemical compound NC(N)=S UMGDCJDMYOKAJW-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- ZFAKTZXUUNBLEB-UHFFFAOYSA-N dicyclohexylazanium;nitrite Chemical compound [O-]N=O.C1CCCCC1[NH2+]C1CCCCC1 ZFAKTZXUUNBLEB-UHFFFAOYSA-N 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011070 membrane recovery Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000010892 non-toxic waste Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 235000021110 pickles Nutrition 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
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- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses an off-line restorative cleaning method of a distributed sewage treatment MBR system, which comprises the steps of emptying a membrane tank of the MBR system by controlling sludge discharge operations of an anoxic tank, an aerobic tank, the membrane tank and a reflux tank of the MBR system, soaking and cleaning a membrane component by preparing alkaline washing liquid/pickling liquid by using produced water of the MBR, and finally discharging the alkaline washing liquid/pickling liquid into a biochemical system for digestion and restoring the operation of the system. The cleaning method is suitable for restoring cleaning of the membrane of the MBR system for distributed sewage treatment, has short cleaning time and high efficiency, cleaning foam generated in the cleaning process cannot overflow and cause pollution to the environment, and cleaning waste liquid cannot cause impact on a biochemical system.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an offline restorative cleaning method of a distributed sewage treatment MBR system.
Background
Sewage treatment systems are generally classified into two types, centralized and decentralized. The centralized sewage treatment system is suitable for treating the wastewater in areas with concentrated pollution sources, and has the characteristics of large treatment scale, high capital construction cost, high operation cost and the like. However, the domestic sewage in suburbs or areas far from cities and towns and not covered in specific areas of municipal pipe network coverage area, such as black and odorous water, sewage interception, pump station forebay sewage, rural and urban-rural junctions, army residence areas, tourist areas, independent villa areas, airports and the like, has the characteristics of small sewage amount, large fluctuation, dispersed generation sources, large pollution sources, unsuitability for centralized treatment and the like. The decentralized treatment, namely on-site treatment and on-site recycling, of the sewage is the key point of the current research and application. Among them, the MBR membrane treatment process has been widely used in the field of sewage treatment, particularly in the treatment of dispersed sewage, due to the characteristics of increased membrane flux, reduced membrane cost, and prolonged life. However, MBR membranes are susceptible to varying degrees of fouling after a period of operation, membrane flux decreases, and periodic restorative cleaning is required.
At present, the membrane offline recovery cleaning of a distributed sewage treatment MBR system mainly has the following problems:
1. off-line restorative cleaning is difficult.
The off-line recovery cleaning comprises two modes, namely taking the membrane assembly out of the membrane pool, soaking the membrane assembly in a cleaning pool filled with chemical cleaning agents (ex-situ off-line recovery cleaning), or evacuating activated sludge in the membrane pool, directly injecting the chemical agents into the membrane pool, soaking the membrane assembly (in-situ off-line recovery cleaning), and the like. Ectopic off-line restorative cleaning is currently studied more. Chinese patent CN206173093U and chinese patent CN205386415U provide two mobile MBR membrane cleaning devices. Utilize the lorry to transport membrane belt cleaning device to the processing point, hoist the membrane module to membrane belt cleaning device by the membrane pond and wash in, solved and returned the problem that membrane silk dehydration that factory off-line recovery nature washing exists scraps the risk high, but multiplied the problem poor to suitability such as the relatively poor mountain and water tourist area of road transportation, washing operation condition, black and odorous water body, pump station forebay simultaneously. In summary, poor applicability, high transportation and hoisting cost and high treatment cost of the cleaning waste liquid are key factors for limiting the large-scale application of ex-situ off-line restorative cleaning.
In-situ offline restorative cleaning circumvents the above-mentioned problems, but at the same time puts new requirements on MBR system design. Chinese patent CN110776091A discloses an immersed MBR in-situ off-line restorative cleaning method without impact on sludge activity: the system is provided with n grids of membrane pools (n is more than or equal to 4), wherein n-1 grid is a working membrane pool, and the rest 1 grid is a vacant membrane pool. When in-situ off-line restorative cleaning is carried out, the cleaning pump firstly pumps sludge in the working membrane pool to be cleaned into the vacant membrane pool, then pumps the cleaning agent in the cleaning agent tank into the working membrane pool to be cleaned, soaks for a certain time, then pumps the reducing agent in the reducing agent tank into the working membrane pool to be cleaned, finally reflows the nontoxic waste liquid to the regulating tank, and pumps the sludge in the vacant membrane pool back to the cleaned working membrane pool. The essence of the method is that the sludge mixed liquid is dispatched through an empty membrane pool, the cleaning water is obtained through n-1 sets of MBR systems which run in parallel, and the waste cleaning liquid is consumed through the reduction of a reducing agent. However, the MBR system with n-1 sets (n is more than or equal to 4) has the lowest economic water yield, is not consistent with the characteristics of small yield and large fluctuation of dispersed sewage, and is difficult to generally apply. The arrangement of the vacant membrane tanks is contrary to the characteristics of dispersed sewage generation sources and large quantity of pollution sources, is low in economical efficiency and is difficult to be generally applied.
Due to the distributed sewage characteristics, the MBR system (especially a single set of MBR system) has the following problems in the in-situ off-line recovery cleaning: (1) the mixed liquid of the membrane pool activated sludge is difficult to transfer; (2) the cleaning water source is difficult to obtain; (2) the cleaning foam is difficult to control and is easy to cause pollution to the environment; (3) the cleaning waste liquid is difficult to treat and is easy to cause impact on a biochemical system.
2. The existing cleaning agent has poor cleaning effect.
The membrane recovery cleaning of the MBR system mostly adopts a cleaning mode combining alkaline cleaning and acid cleaning, the existing alkaline cleaning agent mostly adopts 0.1-0.3% of sodium hypochlorite solution, and the acid cleaning agent mostly adopts 1-3% of citric acid solution. However, with the improvement of effluent standards, the distributed sewage treatment MBR system is increasingly applied to high-efficiency nitrogen and phosphorus removal wastewater treatment, the 'phosphorus removal' is gradually changed from mainly biological phosphorus removal to mainly chemical phosphorus removal, and Fe introduced by a chemical phosphorus removal coagulant3+、Al3+And PO4 3-The plasma is easy to deposit on the surface of the film to form newMembrane contaminants, existing cleaning Agents on Ca2+、Mg2+、Fe3+、Al3+And PO4 3-And the formed pollutants have weak dissolving capacity and poor cleaning effect.
Disclosure of Invention
In order to solve the technical problem, the invention provides an off-line recovery cleaning method of a distributed sewage treatment MBR system.
The technical scheme adopted by the invention is as follows:
an off-line restorative cleaning method of a distributed sewage treatment MBR system comprises an anoxic tank, an aerobic tank, a membrane tank, a reflux tank, a clear water tank and a desliming system which are sequentially connected, wherein an MBR membrane module is arranged in the membrane tank, water produced by the MBR membrane module can enter the reflux tank and the clear water tank through a water production pump, the reflux tank is connected with the anoxic tank through the reflux pump, and the clear water tank is connected with a water production pipe of the MBR membrane module through a chemical cleaning pump; the bottom parts of the anoxic tank, the aerobic tank, the membrane tank, the reflux tank and the clean water tank are all provided with a sludge discharge valve, the sludge discharge valve is connected with a desliming system through a sludge discharge pipe and a sludge discharge pump, and the clean water separated by the desliming system flows back to the anoxic tank through the clean water pump; the off-line cleaning method of the distributed sewage treatment MBR system comprises the following steps that:
step one, emptying a membrane tank by controlling sludge discharge operations of an anoxic tank, an aerobic tank, the membrane tank and a reflux tank while not additionally arranging a cleaning device;
step two, preparing an alkali washing agent by utilizing the produced water of the MBR to carry out alkali washing soaking on the membrane module, and discharging alkali washing waste liquid to a biochemical system for consumption;
step three, preparing a pickling agent by utilizing the produced water of the MBR to carry out pickling and soaking on the membrane module, and discharging pickling waste liquid into a biochemical system for digestion;
and step four, restoring the system operation.
Further, the first step comprises:
1.1) stopping water inflow of the system, opening a mud valve at the bottom of the aerobic tank and the membrane tank, and communicating the two tanks; starting a reflux pump, starting a water production pump, and discharging produced water to a clean water tank; continuously producing water, and stopping the reflux pump when the liquid level of the reflux pool is reduced to the protection liquid level of the reflux pump;
1.2) closing a mud valve at the bottom of the aerobic tank and the membrane tank, opening a mud valve at the bottom of the reflux tank, opening a mud pump, and allowing residual activated sludge mixed liquor in the reflux tank to enter a desliming system through the mud pump. And when the reflux pool is emptied, closing the mud valve at the bottom of the reflux pool. Clear liquid generated by the desliming system is pumped into the anoxic tank by a clear liquid pump;
1.3) opening a mud valve at the bottom of the aerobic tank and the membrane tank, closing a water inlet valve of the clean water tank, opening a water inlet valve of the reflux tank, and discharging produced water to the reflux tank; continuously producing water, closing a water inlet valve of the backflow pool when the liquid level of the backflow pool reaches a high liquid level, opening a water inlet valve of the clean water pool, and discharging the produced water to the clean water pool;
1.4) stopping the water pump when the liquid level in the membrane pool is reduced to 20-30 cm of immersed membrane filaments, and carrying out static pressure water production until the liquid level in the membrane pool submerges the membrane filaments;
1.5) closing a sludge discharge valve at the bottom of the aerobic tank, opening a sludge discharge pump, and allowing residual activated sludge mixed liquor in the membrane tank to enter a desliming system through the sludge discharge pump; and when the membrane tank is emptied, closing a sludge discharge valve at the bottom of the membrane tank, and pumping clear liquid generated by the desliming system into the anoxic tank by a clear liquid pump.
Further, the second step comprises:
2.1) transferring the produced water temporarily stored in the reflux pool to a membrane pool by using a temporary pump, adding an alkali washing agent into the membrane pool, and stopping the temporary pump when the liquid level in the membrane pool submerges 10-15 cm of the top of the membrane wire;
2.2) starting alkaline washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the alkaline washing and soaking process flows into a backflow tank from a membrane tank and is pumped into a desliming system through a sludge discharge pump to be absorbed;
2.3) after the alkali cleaning is finished, determining that the residual chlorine load q is not more than 0.01m3When the water is used for washing, the alkali washing waste liquid in the membrane pool is transferred to an aerobic pool by using a temporary pump for digestion until the membrane pool is emptied;
q＝C1·Q1/M1；
C1the residual chlorine concentration of the alkali washing waste liquid is shown;
M1the concentration of the activated sludge in the aerobic tank;
Q1is the temporary pump flow rate.
Further, the third step comprises:
3.1) starting a chemical cleaning pump, and reversely injecting the produced water temporarily stored in the clean water tank into the membrane tank; adding an acid washing agent into the membrane pool, and stopping the chemical cleaning pump when the liquid level in the membrane pool submerges 10-15 cm of the top of the membrane wire;
3.2) starting acid washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the acid washing and soaking process flows into a reflux pool from a membrane pool and is pumped into a desliming system through a mud pump to be absorbed;
3.3) after the acid washing is finished, transferring the membrane pool acid washing waste liquid to a reflux pool by using a temporary pump, closing the reflux pump, feeding water into the system, and producing water by static pressure;
3.4) transferring the pickling waste liquid in the reflux pool to an anoxic pool by using a temporary pump until the reflux pool is emptied, and adjusting the flow of the temporary pump and the flow of static pressure produced water to ensure that the relative COD concentration R is not more than 0.01;
R＝C2·Q1/Q3·M1
Q1is the temporary pump flow rate;
Q3the water flow is produced by static pressure;
C2the COD concentration of the pickling waste liquid;
M1the concentration of the activated sludge in the aerobic tank.
Further, the fourth step includes: and after the pickling waste liquid is treated, starting a reflux pump, feeding water into a reflux pool, and normally operating the system.
Further, the alkali washing agent is prepared from sodium hypochlorite, a transforming agent, a chelating agent, a surfactant and water; the concentration of sodium hypochlorite in the alkaline cleaning agent is 1000-3000 mg/L, the concentration of the transforming agent is 10-50 mg/L, the concentration of the chelating agent is 10-50 mg/L, and the concentration of the surfactant is 1-10 mg/L.
Further, the conversion agent is selected from at least one of sodium hydroxide, sodium carbonate and sodium bicarbonate; the chelating agent is at least one selected from sodium hexametaphosphate, disodium ethylene diamine tetraacetate and tetrasodium ethylene diamine tetraacetate; the surfactant is at least one selected from nonylphenol polyoxyethylene ether, fatty alcohol polyoxyethylene ether and alkanolamide.
Further, the pickling agent is prepared from citric acid, sulfamic acid, a corrosion inhibitor, a chelating agent, a surfactant and water; the concentration of citric acid in the pickling agent is 1000-3000 mg/L, the concentration of sulfamic acid is 50-100 mg/L, the concentration of corrosion inhibitor is 10-50 mg/L, the concentration of chelating agent is 10-50 mg/L, and the concentration of surfactant is 1-10 mg/L.
Further, the corrosion inhibitor is selected from at least one of amines and thioureas; the chelating agent is at least one selected from sodium tripolyphosphate and ethylene diamine tetraacetic acid; the surfactant is at least one selected from nonylphenol polyoxyethylene ether, fatty alcohol polyoxyethylene ether and alkanolamide.
The invention has the beneficial effects that:
1. the cleaning method can realize the membrane in-situ off-line recovery cleaning of the MBR system for distributed sewage treatment, particularly a single set of MBR system, and cleaning foam cannot overflow in the cleaning process and impact on a biochemical system to influence the recovery operation of the system.
2. The waste liquid generated in the cleaning process of the cleaning solution is not required to be treated by adding an agent, the alkali cleaning waste liquid is transferred to the aerobic tank for consumption, and the acid cleaning waste liquid is transferred to the anoxic tank for consumption, so that the pollution load is reduced.
Drawings
FIG. 1 is a schematic structural diagram of a distributed sewage treatment MBR system of the present invention.
Detailed Description
In order to better understand the present invention, the following examples are further provided to illustrate the present invention, but the present invention is not limited to the following examples.
It should be noted that the chemicals used in the following examples are commercially available.
Example 1
Referring to fig. 1, the embodiment provides an offline restorative cleaning method for a distributed sewage treatment MBR system, where the distributed sewage treatment MBR system includes an anoxic tank 1, an aerobic tank 2, a membrane tank 3, a reflux tank 4, a clean water tank 5, and a desliming system 6, which are connected in sequence, the membrane tank is provided with an MBR membrane module 7, water produced by the MBR membrane module enters the reflux tank 4 and the clean water tank 5 through a water production pump 8, the reflux tank 4 is connected with the anoxic tank 1 through a reflux pump 9, and the clean water tank 5 is connected with a water production pipe of the MBR membrane module 7 through a chemical cleaning pump 10; the bottoms of the anoxic tank 1, the aerobic tank 2, the membrane tank 3, the reflux tank 4 and the clean water tank 5 are respectively provided with a mud valve, the mud valves are connected with a desliming system 7 through mud pipes and a mud pump 11, and the clean water separated by the desliming system flows back to the anoxic tank 1 through a clean water pump 12; an alkali washing box 21 and a pickling box 22 are arranged above the membrane tank 3, the alkali washing box 21 is communicated with the membrane tank 3 through an alkali pump and a valve, and the pickling box 22 is communicated with the membrane tank 3 through an acid pump and a valve.
When the transmembrane pressure difference of the distributed sewage treatment MBR system of the embodiment rises to 30kPa, off-line cleaning is carried out by using a self-prepared cleaning agent, and the off-line cleaning method comprises the following steps:
1) preparing an alkali washing agent: weighing 50g of 10 wt% sodium hypochlorite solution, 0.5g of sodium hydroxide, 0.5g of sodium hexametaphosphate and 0.05g of nonylphenol polyoxyethylene ether, adding water to dilute to 50L, and uniformly mixing for later use. In the alkaline detergent of this example, the concentration of sodium hypochlorite is 1000mg/L, the concentration of transforming agent is 10mg/L, the concentration of chelating agent is 10mg/L, and the concentration of surfactant is 1 mg/L.
2) Preparing an acid washing agent: weighing 50g of citric acid, 2.5g of sulfamic acid, 0.5g of dicyclohexylamine nitrite, 0.5g of sodium tripolyphosphate and 0.05g of nonylphenol polyoxyethylene ether, adding water to dilute to 50L, and uniformly mixing for later use. In the pickling agent of the embodiment, the concentration of citric acid is 1000mg/L, the concentration of sulfamic acid is 50mg/L, the concentration of corrosion inhibitor is 10mg/L, the concentration of chelating agent is 10mg/L, and the concentration of surfactant is 1 mg/L.
3) And emptying the membrane pool:
3.1) stopping water inflow of the system, opening sludge discharge valves at the bottoms of the aerobic tank 2 and the membrane tank 3 and communicating the two tanks; starting a water production pump 8, discharging produced water to a clean water tank 5, and stopping a reflux pump 9 when the liquid level of the reflux tank 4 is reduced to the protection liquid level of the reflux pump 9 after the produced water is continuously produced;
3.2) closing a mud valve at the bottom of the aerobic tank 2 and the membrane tank 3, opening a mud valve at the bottom of the return tank 4, opening a mud pump 11, allowing residual activated sludge mixed liquor in the return tank 4 to enter a desliming system 6 through the mud pump 11 until the return tank 4 is emptied, closing the mud valve at the bottom of the return tank, and pumping clear liquid generated by the desliming system 6 into the anoxic tank 1 through a clear liquid pump 12;
3.3) opening mud valves at the bottoms of the aerobic tank 2 and the membrane tank 3, closing a water inlet valve of a clean water tank 5, opening a water inlet valve of a reflux tank 4, and discharging produced water to the reflux tank 4; when the continuous water production is carried out until the backflow pool 4 reaches a high liquid level, the water inlet valve of the backflow pool 4 is closed, the water inlet valve of the clean water pool 5 is opened, and the produced water is discharged to the clean water pool 5;
3.4) stopping the water pump 8 when the liquid level in the membrane pool 3 is reduced to 20-30 cm of immersed membrane filaments, and carrying out static pressure water production until the liquid level in the membrane pool 3 submerges the membrane filaments;
3.5) closing a sludge discharge valve at the bottom of the aerobic tank 2, starting a sludge discharge pump 11, and allowing the residual activated sludge mixed liquor in the membrane tank 3 to enter a desliming system 6 through the sludge discharge pump 11; when the membrane tank 3 is emptied, closing a sludge discharge valve at the bottom of the membrane tank 3; clear liquid produced by the desliming system 6 is pumped into the anoxic tank 1 by a clear liquid pump 12.
4) And alkali washing and soaking:
4.1) transferring the produced water temporarily stored in the reflux pool 4 to the membrane pool 3 by using a temporary pump 9, adding the alkaline washing agent prepared in the embodiment 1 into the membrane pool 3 through an alkaline washing box and an alkaline pump, and stopping the temporary pump 9 when the liquid level in the membrane pool 3 submerges the top of the membrane wire by 10-15 cm;
4.2) starting alkaline washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the alkaline washing and soaking process flows into the backflow tank 4 from the membrane tank 3 and is pumped into the desliming system 6 through the sludge discharge pump 11 for consumption;
4.3) after the alkali cleaning is finished, measuring the residual chlorine concentration C of the alkali cleaning waste liquid in the membrane pool 3120mg/L, the concentration M of the activated sludge in the aerobic tank 21When the concentration is 10000mg/L, the alkali washing waste liquid in the membrane pool 3 is transferred to the aerobic pool 2 by a temporary pump for absorption until the membrane pool 3 is emptied; during emptying, the temporary pump flow rate Q is adjusted1Is 2m3H, the residual chlorine load q is always lower than 0.01m3/h。
q＝C1·Q1/M1；
C1The residual chlorine concentration of the alkali washing waste liquid is shown;
M1the concentration of the activated sludge in the aerobic tank;
Q1is the temporary pump flow rate.
5) Acid pickling and soaking:
5.1) starting the chemical cleaning pump 10, and reversely injecting the produced water temporarily stored in the clean water tank 5 into the membrane tank 3; adding the acid washing agent prepared in the embodiment 1 into a membrane pool 3 through an acid washing box and an acid pump, and stopping a chemical cleaning pump 10 when the liquid level in the membrane pool submerges the top of a membrane wire by 10-15 cm;
5.2) starting acid washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the acid washing and soaking process flows into a reflux pool 4 through a membrane 3 and is pumped into a desliming system 6 through a sludge discharge pump 11 for consumption;
5.3) after the acid washing is finished, transferring the acid washing waste liquid in the membrane pool 3 to a reflux pool 4 by using a temporary pump, closing a reflux pump 9, feeding water into the system, and producing water by static pressure;
5.4) measuring and detecting the COD concentration C of the pickle liquor2100mg/L, the concentration M of the activated sludge in the aerobic tank 21And when the concentration is 10000mg/L, the acid pickling waste liquid in the reflux pool 4 is transferred to the anoxic pool 1 by using a temporary pump until the reflux pool 4 is emptied. During emptying, the temporary pump flow rate Q is adjusted1Is 2m3Flow rate Q of water produced by static pressure3Is 2m3The relative COD concentration R is always less than 0.01.
R＝C2·Q1/Q3·M1
Q1Is the temporary pump flow rate;
Q3the water flow is produced by static pressure;
C2the COD concentration of the pickling waste liquid;
M1the concentration of the activated sludge in the aerobic tank.
6) And recovering the system: and after the pickling waste liquid is treated, water enters the reflux pool 4, the reflux pump 9 is started, and the system operates normally.
After the system was operated normally for 24 hours, the recovery rate of membrane flux was determined to be 77.6%.
Example 2
Preparing an alkali washing agent: weighing 1500g of 10 wt% sodium hypochlorite solution, 2.5g of sodium carbonate, 0.5g of ethylene diamine tetraacetic acid and 0.5g of alkanolamide, adding water to dilute the mixture to 50L, and uniformly mixing the mixture for later use.
Preparing an acid pickling agent: weighing 150g of citric acid solution, 5g of sulfamic acid, 2.5g of thiourea corrosion inhibitor, 0.5g of ethylene diamine tetraacetic acid and 0.5g of fatty alcohol-polyoxyethylene ether, adding water to dilute to 50L, and uniformly mixing for later use.
The dispersive type sewage treatment MBR system shown in FIG. 1 is subjected to off-line recovery cleaning by using the cleaning agent prepared in example 2 in the same way as in example 1, and the recovery rate of membrane flux is determined to be 88.2% after the system normally operates for 24 hours.
Example 3
Preparing an alkali washing agent: the same raw material components as those in example 3 were used to prepare alkaline and acid detergents, in which the sodium hypochlorite concentration was 1500mg/L, the conversion agent concentration was 30mg/L, the chelating agent concentration was 30mg/L, and the surfactant concentration was 5 mg/L. In the pickling agent of this example, the concentration of citric acid was 2000mg/L, the concentration of sulfamic acid was 70mg/L, the concentration of corrosion inhibitor was 20mg/L, the concentration of chelating agent was 20mg/L, and the concentration of surfactant was 5 mg/L.
The dispersive type sewage treatment MBR system shown in FIG. 1 was cleaned off-line by the same method as in example 1 using the cleaning agent prepared in example 3, and the recovery rate of membrane flux was determined to be 80.4% after the system normally operated for 24 hours.
Comparative example 1
The distributed sewage treatment MBR system shown in fig. 1 was off-line cleaned using commercially available alkaline cleaning solutions and acidic cleaning solutions in the same manner as in example 1, and the membrane flux was measured to return to 65.6% after the system normally operated for 24 hours.
As can be seen from the above examples and comparative examples, the cleaning effect of the cleaning agent prepared by the invention for off-line cleaning of the MBR system is much higher than that of the existing cleaning solution.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. An off-line restorative cleaning method of a distributed sewage treatment MBR system comprises an anoxic tank, an aerobic tank, a membrane tank, a reflux tank, a clear water tank and a desliming system which are sequentially connected, wherein an MBR membrane module is arranged in the membrane tank, water produced by the MBR membrane module enters the reflux tank and the clear water tank through a water production pump, the reflux tank is connected with the anoxic tank through a reflux pump, and the clear water tank is connected with a water production pipe of the MBR membrane module through a chemical cleaning pump; the bottom parts of the anoxic tank, the aerobic tank, the membrane tank, the reflux tank and the clean water tank are all provided with a sludge discharge valve, the sludge discharge valve is connected with a desliming system through a sludge discharge pipe and a sludge discharge pump, and the clean water separated by the desliming system flows back to the anoxic tank through the clean water pump; the method is characterized in that: the off-line cleaning method of the distributed sewage treatment MBR system comprises the following steps that:
step one, emptying a membrane tank by controlling sludge discharge operations of an anoxic tank, an aerobic tank, the membrane tank and a reflux tank while not additionally arranging a cleaning device;
step two, preparing an alkali washing agent by utilizing the produced water of the MBR to carry out alkali washing soaking on the membrane module, and discharging alkali washing waste liquid to a biochemical system for consumption;
step three, preparing a pickling agent by utilizing the produced water of the MBR to carry out pickling and soaking on the membrane module, and discharging pickling waste liquid into a biochemical system for digestion;
and step four, restoring the system operation.
2. The off-line restorative cleaning method of claim 1, wherein step one comprises:
1.1) stopping water inflow of the system, opening sludge discharge valves at the bottoms of the aerobic tank and the membrane tank, and communicating the two tanks; starting a water production pump, discharging produced water to a clean water tank, and stopping a reflux pump when the liquid level of the reflux tank is reduced to the protective liquid level of the reflux pump after the produced water is continuously produced;
1.2) closing a mud valve at the bottom of the aerobic tank and the membrane tank, opening a mud valve at the bottom of the reflux tank, opening a mud pump, allowing residual activated sludge mixed liquor in the reflux tank to enter a desliming system through the mud pump until the reflux tank is emptied, closing the mud valve at the bottom of the reflux tank, and pumping clear liquid generated by the desliming system into an anoxic tank through a clear liquid pump;
1.3) opening a mud valve at the bottom of the aerobic tank and the membrane tank, closing a water inlet valve of the clean water tank, opening a water inlet valve of the reflux tank, and discharging produced water to the reflux tank; continuously producing water, closing a water inlet valve of the backflow pool when the backflow pool reaches a high liquid level, opening a water inlet valve of the clean water pool, and discharging the produced water to the clean water pool;
1.4) stopping the water pump when the liquid level in the membrane pool is reduced to 20-30 cm of immersed membrane filaments, and carrying out static pressure water production until the liquid level in the membrane pool submerges the membrane filaments;
1.5) closing a sludge discharge valve at the bottom of the aerobic tank, opening a sludge discharge pump, and allowing residual activated sludge mixed liquor in the membrane tank to enter a desliming system through the sludge discharge pump; and when the membrane tank is emptied, closing a sludge discharge valve at the bottom of the membrane tank, and pumping clear liquid generated by the desliming system into the anoxic tank by a clear liquid pump.
3. The off-line restorative cleaning method of claim 1 or 2, wherein step two comprises:
2.1) transferring the produced water temporarily stored in the reflux pool to a membrane pool by using a temporary pump, adding an alkali washing agent into the membrane pool, and stopping the temporary pump when the liquid level in the membrane pool submerges 10-15 cm of the top of the membrane wire;
2.2) starting alkaline washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the alkaline washing and soaking process flows into a backflow tank from a membrane tank and is pumped into a desliming system through a sludge discharge pump to be absorbed;
2.3) after the alkali cleaning is finished, determining that the residual chlorine load q is not more than 0.01m3When the water is used for washing, the alkali washing waste liquid in the membrane pool is transferred to an aerobic pool by using a temporary pump for digestion until the membrane pool is emptied;
q＝C1·Q1/M1；
C1the residual chlorine concentration of the alkali washing waste liquid is shown;
M1the concentration of the activated sludge in the aerobic tank;
Q1is the temporary pump flow rate.
4. The off-line restorative cleaning method of claim 1 or 2, wherein step three comprises:
3.1) starting a chemical cleaning pump, and reversely injecting the produced water temporarily stored in the clean water tank into the membrane tank; adding an acid washing agent into the membrane pool, and stopping the chemical cleaning pump when the liquid level in the membrane pool submerges 10-15 cm of the top of the membrane wire;
3.2) starting acid washing and soaking, wherein the soaking time is controlled to be 8-12 h, and cleaning foam generated in the acid washing and soaking process flows into a reflux pool from a membrane pool and is pumped into a desliming system through a mud pump to be absorbed;
3.3) after the acid washing is finished, transferring the membrane pool acid washing waste liquid to a reflux pool by using a temporary pump, closing the reflux pump, feeding water into the system, and producing water by static pressure;
3.4) transferring the pickling waste liquid in the reflux pool to an anoxic pool by using a temporary pump until the reflux pool is emptied, and adjusting the flow of the temporary pump and the flow of static pressure produced water to ensure that the relative COD concentration R is not more than 0.01;
R＝C2·Q1/Q3·M1
Q1is the temporary pump flow rate;
Q3the water flow is produced by static pressure;
C2the COD concentration of the pickling waste liquid;
M1the concentration of the activated sludge in the aerobic tank.
5. The off-line restorative cleaning method of claim 1 or 2, wherein step four comprises: and after the pickling waste liquid is treated, starting a reflux pump, feeding water into a reflux pool, and normally operating the system.
6. The off-line restorative cleaning method of claim 1, wherein the alkaline detergent is formulated from sodium hypochlorite, a converting agent, a chelating agent, a surfactant, and water; the concentration of sodium hypochlorite in the alkaline cleaning agent is 1000-3000 mg/L, the concentration of the transforming agent is 10-50 mg/L, the concentration of the chelating agent is 10-50 mg/L, and the concentration of the surfactant is 1-10 mg/L.
7. The off-line restorative cleaning method of claim 6, wherein the conversion agent is selected from at least one of sodium hydroxide, sodium carbonate, and sodium bicarbonate; the chelating agent is at least one selected from sodium hexametaphosphate, disodium ethylene diamine tetraacetate and tetrasodium ethylene diamine tetraacetate; the surfactant is at least one selected from nonylphenol polyoxyethylene ether, fatty alcohol polyoxyethylene ether and alkanolamide.
8. The off-line restorative cleaning method of claim 1, wherein the acid cleaning agent is formulated from citric acid, sulfamic acid, a corrosion inhibitor, a chelating agent, a surfactant, and water; the concentration of citric acid in the pickling agent is 1000-3000 mg/L, the concentration of sulfamic acid is 50-100 mg/L, the concentration of corrosion inhibitor is 10-50 mg/L, the concentration of chelating agent is 10-50 mg/L, and the concentration of surfactant is 1-10 mg/L.
9. The off-line restorative cleaning method of claim 8, wherein the corrosion inhibitor is selected from at least one of amines and thioureas; the chelating agent is at least one selected from sodium tripolyphosphate and ethylene diamine tetraacetic acid; the surfactant is at least one selected from nonylphenol polyoxyethylene ether, fatty alcohol polyoxyethylene ether and alkanolamide.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114920356A (en) * | 2022-06-10 | 2022-08-19 | 青岛双元水务有限公司 | Intelligent cleaning method for MBR (membrane bioreactor) |
| CN115925099A (en) * | 2022-11-09 | 2023-04-07 | 天津绿缘环保工程股份有限公司 | Skid-mounted MBR (membrane bioreactor) membrane cleaning and recycling device and cleaning method |
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2020
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114920356A (en) * | 2022-06-10 | 2022-08-19 | 青岛双元水务有限公司 | Intelligent cleaning method for MBR (membrane bioreactor) |
| CN114920356B (en) * | 2022-06-10 | 2023-06-16 | 青岛水务集团有限公司 | Intelligent cleaning method for MBR (Membrane bioreactor) |
| CN115925099A (en) * | 2022-11-09 | 2023-04-07 | 天津绿缘环保工程股份有限公司 | Skid-mounted MBR (membrane bioreactor) membrane cleaning and recycling device and cleaning method |
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