CN113101811B - Recovery cleaning method for MBR hollow fiber membrane - Google Patents
Recovery cleaning method for MBR hollow fiber membrane Download PDFInfo
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- CN113101811B CN113101811B CN202110581692.3A CN202110581692A CN113101811B CN 113101811 B CN113101811 B CN 113101811B CN 202110581692 A CN202110581692 A CN 202110581692A CN 113101811 B CN113101811 B CN 113101811B
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/02—Hollow fibre modules
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/162—Use of acids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/164—Use of bases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/20—By influencing the flow
- B01D2321/2033—By influencing the flow dynamically
- B01D2321/2058—By influencing the flow dynamically by vibration of the membrane, e.g. with an actuator
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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
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- C02F2303/14—Maintenance of water treatment installations
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
The invention relates to a recovery cleaning method for an MBR hollow fiber membrane. The method comprises the following steps: emptying the reaction chamber, removing the MBR hollow fiber membrane filter cake layer, and injecting clear water into the reaction chamber; considering the inside and outside of the hollow fiber membrane and concentration polarization, adding a cleaning agent into the reaction chamber, simultaneously introducing the cleaning agent/water into the MBR hollow fiber membrane in a back flushing mode, and along with aeration, wherein the concentration of the cleaning agent in the MBR hollow fiber membrane is less than that of the cleaning agent in the reaction chamber; then stopping adding the cleaning agent into the reaction chamber, keeping aeration and introducing the cleaning agent/water into the hollow fiber membrane in a backflushing mode; then stopping aeration and introducing cleaning agent/water into the MBR hollow fiber membrane in a backflushing mode, and performing 'water-gas cooperative cleaning' of soaking, backflushing, soaking and aeration alternately. The method can realize the high-efficiency recovery of the MBR hollow fiber membrane flux, has lasting operation, reduces the recovery cleaning frequency and prolongs the service life.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a recovery cleaning method for an MBR hollow fiber membrane.
Background
In recent years, the requirement of water environment treatment is further improved, and a lot of regions propose that part of indexes of town sewage treatment need to meet the requirements of IV or III class water quality in surface water environment quality standard, and put higher requirements on sewage treatment processes. The Membrane Bioreactor (MBR) is widely applied to the field of sewage treatment due to the characteristics of high effluent quality, stable structure, simple and convenient operation and the like. However, when the MBR treatment technology is used, pollution is formed due to adsorption and deposition on the surface of the membrane and in the membrane pores, concentration polarization is generated, a gel layer is formed, membrane flux is reduced, transmembrane pressure difference is increased, and normal operation of the MBR membrane is affected. Membrane fouling is often mitigated by the use of maintenance or restorative cleaning, where restorative cleaning is directly related to membrane performance and lifetime. The conventional restorative cleaning method at the present stage adopts a medicament dumping injection and whole-course aeration mode, so that the energy consumption of restorative cleaning is greatly increased, meanwhile, the influence of pH on sodium hypochlorite serving as a common alkali cleaning medicament is large, active groups in the alkali cleaning medicament can be decomposed by long-time aeration, the medicament property is reduced, the cleaning medicament is wasted, the pH is often required to be adjusted in the cleaning process, and a large amount of pH regulators are required to be used. The high energy consumption and drug consumption greatly improve the water treatment cost, increase the burden of water treatment enterprises and waste resources, so that a low-energy-consumption and high-efficiency MBR hollow fiber membrane restorative cleaning method is urgently needed.
Disclosure of Invention
The invention provides a recovery cleaning method of an MBR hollow fiber membrane, which strives to realize the high-efficiency recovery of the flux of the MBR hollow fiber membrane and protect membrane filaments at the same time.
The technical scheme adopted by the invention is as follows:
a recovery cleaning method for an MBR hollow fiber membrane specifically comprises the following steps:
step 1: stopping discharging water from the MBR hollow fiber membrane to be cleaned, emptying the reaction chamber, cleaning a filter cake layer of the MBR hollow fiber membrane, and injecting clear water until membrane filaments are immersed;
step 2: considering the internal and external parts and concentration polarization of the MBR hollow fiber membrane, adding a cleaning agent into the reaction chamber, introducing the cleaning agent/water into the MBR hollow fiber membrane in a back flushing mode, and aerating in the reaction chamber, wherein the concentration of the cleaning agent in the MBR hollow fiber membrane is less than that of the cleaning agent in the reaction chamber; then, stopping adding the cleaning agent into the reaction chamber, but continuously aerating, and continuously introducing the cleaning agent/water into the MBR hollow fiber membrane in a back flushing manner; then stopping aeration of the reaction chamber, stopping introducing cleaning agent/water into the MBR hollow fiber membrane in a back flushing mode, and soaking for 30-180 min;
and step 3: after soaking, introducing a cleaning agent/water into the MBR hollow fiber membrane 2 for backwashing for 20-60 min;
and 4, step 4: after the back washing is stopped, soaking for 30-180 min;
and 5: after soaking, aerating the reaction chamber for 20-60 min;
step 6: stopping the aeration of the reaction chamber, and soaking for 30-180 min;
and 7: optionally, repeating steps 3-6.
Preferably, the method for cleaning the cake layer of the MBR hollow fiber membrane in step 1 is at least one of in-situ high-pressure water cleaning, blowing and removing by a blower, and ex-situ high-pressure water cleaning.
Preferably, the step 2 comprises two forms of adding cleaning agent through the dispersed pressure holes and introducing the cleaning agent into the MBR membrane in a back flushing mode after the concentration of the cleaning agent is adjusted in the pipeline through back flushing water, and the concentration of the cleaning agent added through the dispersed pressure holes is higher than that of the cleaning agent adjusted through the back flushing water.
Preferably, the cleaning in the steps 3-6 is in-situ cleaning, the cleaning process is a cleaning agent/water back-flushing vibration process, a soaking process, an aeration process and a soaking water-gas cooperation process, and the sequence and duration of each stage can be adjusted according to actual conditions.
Preferably, the cleaning agent in the step 2 is an alkaline cleaning agent or an acid cleaning agent, the cleaning agent in the step 2 is an acid cleaning process when the cleaning agent is an acid cleaning agent, the cleaning agent in the step 2 is an alkaline cleaning process when the cleaning agent is an alkaline cleaning agent, and the MBR hollow fiber membrane restorative cleaning method is suitable for any one of only acid cleaning or only alkaline cleaning, or alkaline cleaning before acid cleaning, or acid cleaning after acid cleaning.
Preferably, when the step 2 is an alkaline cleaning agent, the concentration of the alkaline cleaning agent in the reaction chamber is kept at 1500-5000ppm, and the pH is adjusted to 10-12.
Preferably, when the step 2 is the acid washing agent, the concentration of the acid washing agent in the reaction chamber is 1.5-3 wt%.
A recovery cleaning device for an MBR hollow fiber membrane comprises a reaction chamber, wherein an MBR hollow fiber membrane is arranged in the reaction chamber, a water distribution pipe is arranged below the MBR hollow fiber membrane, a water flow direction outlet of the water distribution pipe points to the inner surface of the MBR hollow fiber membrane, and the water distribution pipe is communicated with a back washing pump; the internal flow channel of the MBR hollow fiber membrane is sequentially communicated with a first alkaline agent dosing pump and an alkaline washing agent storage tank, the alkaline washing agent storage tank is simultaneously communicated with a second alkaline agent dosing pump, and the second alkaline agent dosing pump is communicated with a dosing port of the reaction chamber; the internal flow channel of the MBR hollow fiber membrane is sequentially communicated with a first acid agent dosing pump and an acid washing agent storage tank, the acid washing agent storage tank is simultaneously communicated with a second acid agent dosing pump, and the second acid agent dosing pump is communicated with a dosing port of the reaction chamber; the bottom of the reaction chamber is provided with an aeration device, and the aeration device is connected with an aeration blower.
Preferably, the MBR hollow fiber membrane is further connected with a blowing fan, and the upper part of the MBR hollow fiber membrane is further connected with a water producing pump.
Preferably, the reaction chamber is provided with a vent valve and an exhaust port, and the reaction chamber is further provided with a pH meter.
Preferably, the dosing port of the reaction chamber is communicated with an alkaline medicament pipeline and an acidic medicament pipeline which are arranged in the reaction chamber, and a plurality of dispersed pressure holes are uniformly distributed on the alkaline medicament pipeline and the acidic medicament pipeline.
The invention has the beneficial effects that:
1. the invention realizes the selection of MBR hollow fiber membrane in-situ and ex-situ cleaning.
2. The invention realizes the purpose of adjusting the concentration of the medicament in the reaction chamber, and the cleaning process can realize the addition of one medicament concentration in two concentrations and forms in the device.
3. The invention realizes the water-gas cooperative cleaning with strong and weak collocation alternately carried out by aeration and internal back-flushing vibration, and mixes the cleaning agent by utilizing the physical action of the water-gas cooperative cleaning with strong and weak collocation, thereby maximally utilizing the physical and chemical cleaning capability, reducing the usage amount of the pH regulator, achieving the purpose of reducing the drug consumption under the condition of recovering the same membrane flux, and simultaneously reducing the influence of chemical agents on the structure of biological flora.
4. The aeration and the internal back-flushing vibration of the invention realize the rapid mixing of the cleaning agent, prevent the electric energy loss caused by the whole aeration process and realize the purpose of reducing the energy consumption under the condition of recovering the same membrane flux.
5. The invention realizes the effective separation of the pollutants on the surface of the membrane and the pollutants in the membrane pores from the membrane filaments by the backwashing vibration after soaking.
6. The invention realizes the synergy of membrane surface aeration and membrane filament internal recoil vibration, considers the phenomena of MBR membrane internal, external and concentration polarization, and reduces transmembrane pressure difference increase and membrane flux reduction caused by concentration polarization in an 'internal + external' interconnection and intercommunication mode.
7. The invention realizes 'water-gas cooperation' cleaning by matching aeration with internal backwashing vibration, considers the characteristics and concentration polarization of the MBR hollow fiber membrane and reduces the damage of strong force and high-concentration medicament to the MBR hollow fiber membrane in the backwashing process.
Drawings
FIG. 1 is a schematic diagram of the arrangement of the apparatus of the present invention;
FIG. 2 is a flow control facility of the present invention;
FIG. 3 is a schematic diagram of the backwash water flow and aeration cross flow of the apparatus of the present invention;
FIG. 4 is a time-pressure difference across the membrane plot of example 1;
FIG. 5 is a graph of time versus pressure difference across a membrane for comparative example 1;
FIG. 6 is a time-transmembrane pressure difference graph of comparative example 2;
FIG. 7 is a time-transmembrane pressure difference graph of comparative example 3.
Wherein, the names corresponding to the reference numbers are: 1-a reaction chamber, 2-an MBR hollow fiber membrane, 3-a water distribution pipe, 4-a backwash pump, 5-a backwash flowmeter, 6-a backwash valve, 7-an emptying valve, 8-an emptying flowmeter, 9-an alkaline washing agent storage tank, 10-a first alkaline agent dosing pump, 11-a first alkaline agent flow control facility, 12-a second alkaline agent dosing pump, 13-a second alkaline agent flow control facility, 14-an acid washing agent storage tank, 15-a first acid agent dosing pump, 16-a first acid agent flow control facility, 17-a second acid agent dosing pump, 18-a second acid agent flow control facility, 19-a pH meter, 20-a water production pump, 21-a water production flow control facility, 22-an aeration device, 23-an aeration blower and 24-an aeration flowmeter, 25-an aeration valve, 26-a blowing fan, 27-a blowing fan flowmeter, 28-a blowing fan valve, 29-an exhaust port, 30-a dosing port, 31-an alkaline medicament pipeline, 32-an acidic medicament pipeline, 33-a flowmeter, 34-a pressure sensor and 35-a valve.
Detailed Description
Aiming at the problems of high energy consumption and large medicament dosage in the recovery cleaning method of the MBR hollow fiber membrane in the prior art, the invention provides a low-energy-consumption and high-efficiency recovery cleaning method of the MBR hollow fiber membrane, which comprises the following steps:
step 1: stopping discharging water from the MBR hollow fiber membrane 2 to be cleaned, emptying the reaction chamber 1, cleaning a filter cake layer of the MBR hollow fiber membrane 2, and injecting clear water until the MBR hollow fiber membrane 2 is immersed;
step 2: adding a cleaning agent into the reaction chamber, simultaneously introducing the cleaning agent/water into the MBR hollow fiber membrane 2 in a backflushing mode, aerating in the reaction chamber, wherein the concentration of the cleaning agent in the MBR hollow fiber membrane 2 is less than that of the cleaning agent in the reaction chamber; subsequently, the cleaning agent is stopped being added into the reaction chamber, but aeration is continued, and meanwhile, the cleaning agent/water is continuously introduced into the MBR hollow fiber membrane 2 in a back flushing mode; then, stopping aeration of the reaction chamber, stopping introducing cleaning agent/water into the MBR hollow fiber membrane 2 in a back flushing mode, and soaking for 30-180 min;
and step 3: after soaking, introducing a medicament/water into the MBR hollow fiber membrane 2 for backwashing for 20-60 min;
and 4, step 4: after the back washing is stopped, soaking for 30-180 min;
and 5: after soaking, aerating the reaction chamber 1 for 20-60 min;
step 6: stopping the aeration of the reaction chamber 1, and soaking for 30-180 min;
and 7: optionally, repeating steps 3-6.
In the method, the concentration adjustment of the added cleaning agent is realized in the device, the aeration and the back-flushing vibration are alternately carried out, the strong and weak matched water-gas cooperative cleaning is realized, the physical and chemical cleaning capability can be maximally utilized, and compared with the electric energy loss caused by the whole aeration in the prior art, the method has the advantages that the consumed energy consumption is lower under the condition of realizing the recovery of the same membrane flux; the physical action of strong and weak matching 'water-gas synergy' can effectively mix the cleaning agent, reduce the usage amount of the pH value regulator, realize the purpose of reducing the medicine consumption under the condition of recovering the same membrane flux, and simultaneously reduce the influence of chemical reagents on the structure of biological flora.
Meanwhile, 30-180min of soaking is arranged between the aeration and the backflushing vibration processes, and pollutants generated by soaking can be effectively separated from the membrane wires by the backflushing vibration after soaking.
Meanwhile, the characteristics of the MBR hollow fiber membrane are considered, membrane surface aeration and membrane filament internal backflushing vibration are combined, concentration polarization phenomenon is considered, transmembrane pressure difference increase and membrane flux reduction caused by concentration polarization are reduced in an internal and external intercommunication interconnection mode, and damage of strong force and high-concentration agents to the MBR hollow fiber membrane in the backwashing process is reduced.
Further, when the transmembrane pressure difference of the MBR hollow fiber membrane 2 exceeds 40kPa, the MBR hollow fiber membrane recovery cleaning is performed.
Further, the method for cleaning the cake layer of the MBR hollow fiber membrane 2 in the step 1 is at least one of in-situ high-pressure water cleaning, blowing and removing by a blowing fan and ex-situ high-pressure water cleaning.
The ectopic high-pressure cleaning mode is that the MBR hollow fiber membrane 2 is taken out, the filter cake layer is cleaned by a high-pressure water gun, and the cleaned MBR hollow fiber membrane 2 assembly is placed in the reaction chamber 1.
The in-situ high-pressure cleaning is to clean the filter cake layer 2 of the MBR hollow fiber membrane by using a high-pressure water gun in the reaction chamber 1, and meanwhile, the filter cake layer is swept and removed by using a sweeping fan, and the reaction chamber 1 is emptied after cleaning.
Furthermore, the application of the cleaning agent in the step 2 comprises two forms of adding the cleaning agent through dispersed pressure holes and introducing the cleaning agent into the membrane of the MBR in a back washing mode after the concentration of the cleaning agent is adjusted in the pipeline through back washing water, wherein the concentration of the cleaning agent added through the dispersed pressure holes is higher than that of the cleaning agent adjusted through the back washing water.
Furthermore, the cleaning process in the steps 3-6 is a cyclic 'water-gas cooperation' process of cleaning agent/water back flushing vibration, soaking, aeration and soaking, and the sequence and duration of each stage can be adjusted according to actual conditions.
Further, the cleaning agent in the step 2 is an alkaline cleaning agent or an acid cleaning agent. Specifically, the alkaline cleaning agent is at least one of sodium chlorate, potassium hypochlorite and hydrogen peroxide; the acid-washing agent is at least one of citric acid, oxalic acid and oxalic acid.
Further, when the cleaning agent in the step 2 is an acid cleaning agent, an acid cleaning process is performed, and when the cleaning agent in the step 2 is an alkali cleaning agent, an alkali cleaning process is performed. According to actual conditions, the recovery cleaning mode of the MBR hollow fiber membrane 2 is selected, and can be an acid cleaning process, an alkali cleaning process, an acid cleaning process and an alkali cleaning process, or an alkali cleaning process and an acid cleaning process.
Further, when the step 2 is an alkaline cleaning agent, the concentration of the alkaline cleaning agent in the reaction chamber 1 is kept at 1500-.
Further, when the step 2 is the pickling agent, the concentration of the pickling agent in the reaction chamber 1 is 1.5-3 wt%.
Further, in the step 2, the time for adding the cleaning agent into the reaction chamber 1 is 1-10min, and the time for introducing the cleaning agent and water or water back washing into the MBR hollow fiber membrane 2 is 20-60 min.
The application also provides a MBR hollow fiber membrane recoverability belt cleaning device, and the concrete structure is as follows: the device comprises a reaction chamber 1, wherein an MBR hollow fiber membrane 2 is arranged in the reaction chamber 1, a water distribution pipe 3 is arranged below the MBR hollow fiber membrane 2, a water flow direction outlet of the water distribution pipe 3 points to the inner surface of the MBR hollow fiber membrane 2, and the water distribution pipe 3 is communicated with a back washing pump 4; the internal flow channel of the MBR hollow fiber membrane 2 is sequentially communicated with a first alkaline agent dosing pump 10 and an alkaline washing agent storage tank 9, the other end of the alkaline washing agent storage tank 9 is communicated with a second alkaline agent dosing pump 12, and the second alkaline agent dosing pump 12 is communicated with a dosing port 30 of the reaction chamber 1; the internal flow channel of the MBR hollow fiber membrane 2 is sequentially communicated with a first acid agent dosing pump 15 and an acid washing agent storage tank 14, the other end of the acid washing agent storage tank 14 is communicated with a second acid agent dosing pump 17, and the second acid agent dosing pump 17 is communicated with a dosing port 30 of the reaction chamber 1; the bottom of the reaction chamber 1 is also provided with an aeration device 22, and the aeration device 22 is connected with an aeration blower 23.
In the invention, when the device is used for carrying out alkali cleaning, the reaction chamber 1 is emptied, the filter cake layer of the MBR hollow fiber membrane 2 is cleaned, clear water is injected until the MBR hollow fiber membrane 2 is immersed, when an alkali cleaning process is required, an alkali cleaning agent in an alkali cleaning agent storage tank 9 is added into the reaction chamber 1 through a second alkali agent dosing pump 12, and meanwhile, an aeration blower 23 is opened, and aeration is carried out in the reaction chamber 1 through an aeration device 22; simultaneously, mixing the agent of an alkaline washing agent storage tank 9 and backwashing water in a water distribution pipe 3 through a first alkaline agent dosing pump 10 and a backwashing water pump 4, introducing the mixture into an MBR hollow fiber membrane 2 in a backwashing manner, wherein the concentration of the alkaline washing agent in the MBR hollow fiber membrane 2 is less than that of the alkaline washing agent in a reaction chamber 1, starting a second alkaline agent dosing pump 12 for 1-10min, then closing the second alkaline agent dosing pump, and stopping adding the alkaline washing agent into the reaction chamber 1; the first alkaline agent dosing pump 10 and the backwashing water pump 4 are started for 20-60min and then closed, the alkaline cleaning agent is stopped to be fed into the MBR hollow fiber membrane 2 in a backwashing mode, the aeration blower 23 is closed, the concentration of the alkaline cleaning agent in the reaction chamber 1 is kept at 1500-5000ppm, the pH value is adjusted to 10-12 after the feeding is finished, after soaking is performed for 30-180min, the first alkaline agent dosing pump 10 and the backwashing pump 4 are started to perform backwashing vibration cleaning, after the backwashing vibration cleaning is performed for 20-60min, the first alkaline agent dosing pump 10 and the backwashing pump 4 are closed to be soaked for 30-180min, the aeration blower 23 is started to perform aeration in the reaction chamber 1, after the backwashing vibration cleaning is performed for 20-60min, the soaking is performed for 30-180min, and according to actual conditions, the backwashing vibration, the soaking, the aeration and the soaking procedures are repeated, so that the strong-weak cooperation type cleaning with water and water vapor is realized.
Similarly, when acid cleaning is carried out, the acid cleaning agent in the acid cleaning agent storage tank 14 is added into the reaction chamber 1 through the second acid agent adding pump 17, meanwhile, the acid cleaning agent in the acid cleaning agent storage tank 14 and backwashing water are mixed in the water distribution pipeline 3 through the first acid agent adding pump 15, the mixture is introduced into the MBR hollow fiber membrane 2 in a backwashing mode, and other operation processes are carried out with alkali cleaning.
Further, the MBR hollow fiber membrane 2 is also connected with a sweeping fan 26, and the upper part of the MBR hollow fiber membrane 2 is also connected with a water producing pump 20. The MBR hollow fiber membrane 2 is also connected with a purging fan 26 and is used for purging and removing a filter cake layer of the MBR hollow fiber membrane 2 after in-situ cleaning, and meanwhile, a purging fan flowmeter 27 and a purging fan valve 28 are connected between the MBR hollow fiber membrane 2 and the purging fan 26 and are used for controlling the purging fan 26 to be switched on and off and adjusted; but when the ectopic cleaning mode is adopted, the purging fan does not need to be installed. In addition, the upper part of the MBR hollow fiber membrane 2 is also connected with a water production pump 20, and is used for injecting clear water to immerse the MBR hollow fiber membrane 2 in the emptying reaction chamber 1, and meanwhile, a water production flow control facility 21 is arranged between the MBR hollow fiber membrane 2 and the water production pump 20 and is used for controlling the flow of the produced water.
Further, the reaction chamber 1 is provided with a vent valve 7 and an exhaust port 29, and the reaction chamber 1 is also provided with a pH meter 19. The reaction chamber 1 is provided with an emptying valve 7 and an exhaust port 29 for emptying the liquid in the reaction chamber 1 and exhausting the gas in the reaction chamber 1, and the emptying valve 7 is also communicated with an emptying flowmeter 8 for detecting the flow rate when the liquid is exhausted. In addition, the reaction chamber 1 is provided with a pH meter 19 for detecting the pH value in the reaction chamber 1.
Further, a chemical adding port 30 of the reaction chamber 1 is communicated with an alkaline chemical pipeline 31 and an acidic chemical pipeline 32 which are arranged in the reaction chamber 1 and used for introducing an alkaline cleaning chemical or an acid cleaning chemical into the reaction chamber 1, and meanwhile, a plurality of dispersing holes are uniformly distributed in the alkaline chemical pipeline 31 and the acidic chemical pipeline 32, so that multipoint distribution chemical adding can be realized.
Further, the use of the cleaning agent comprises two forms of adding the cleaning agent through the dispersed pressure holes 31 or 32 and introducing the cleaning agent into the MBR membrane 2 in a back flushing mode after adjusting the concentration of the cleaning agent in the pipeline 3 through back flushing water, wherein the concentration of the cleaning agent added through the dispersed pressure holes is higher than that of the cleaning agent adjusted through the back flushing water.
Furthermore, the cleaning process in the steps 3-6 is a cyclic 'water-gas cooperation' process of cleaning agent/water back flushing vibration, soaking, aeration and soaking, and the sequence and duration of each stage can be adjusted according to actual conditions.
Furthermore, a back-washing flow meter 5 and a back-washing valve 6 are arranged between the water distribution pipe 3 and the back-washing pump 4 and are used for adjusting the back-washing flow. Further, a first alkaline agent flow control facility 11 is arranged between the first alkaline agent dosing pump 10 and the MBR hollow fiber membrane 2 and is used for controlling the adding amount of an alkaline detergent to the MBR hollow fiber membrane 2; a second alkaline agent flow control facility 13 is arranged between the second alkaline agent dosing pump 12 and the reaction chamber 1 and is used for controlling the adding amount of the alkaline cleaning agent into the reaction chamber 1; similarly, a first acid agent flow control facility 16 is arranged between the first acid agent dosing pump 15 and the MBR hollow fiber membrane 2 and is used for controlling the adding amount of the acid washing agent to the MBR hollow fiber membrane 2; a second acid agent flow control device 18 is arranged between the second acid agent dosing pump 17 and the reaction chamber 1 and is used for controlling the adding amount of the acid washing agent into the reaction chamber 1.
In the present invention, the water production flow rate control means 21, the first alkaline agent flow rate control means 11, the second alkaline agent flow rate control means 13, the first acid agent flow rate control means 16, and the second acid agent flow rate control means 18 are common flow rate control devices, and each of them includes a pressure sensor 34, a valve 35, and a flow meter 33, which are sequentially arranged. Flow control means well known in the art are not described in detail herein.
Further, an aeration flow meter 24 and an aeration valve 25 are arranged between the aeration blower 23 and the aeration device 22 for controlling the aeration degree.
The following experiments were carried out using the above method and apparatus:
example 1
When transmembrane pressure difference exceeds 40kPa, emptying the reaction chamber 1, cleaning an MBR hollow fiber membrane 2 in situ by using a high-pressure water gun and a blowing fan, feeding water until membrane filaments are basically immersed, opening a second alkaline agent dosing pump 12 and a second alkaline agent flow control facility 13 to add sodium hypochlorite solution in an alkaline agent storage tank 9 into the reaction chamber 1 in a multipoint distribution dosing mode, simultaneously opening a backwashing pump 4 and a backwashing valve 6, opening a first alkaline agent dosing pump 10 and a first alkaline agent flow control facility 11 to mix the sodium hypochlorite solution in the alkaline agent storage tank 9 with water in a water distribution pipeline, introducing the mixed solution into the MBR hollow fiber membrane 2 in a backwashing mode, simultaneously opening an aeration blower 23 and a valve 25, closing the second alkaline agent dosing pump 12 after 5min, keeping the effective chlorine concentration of the reaction chamber 1 at 2500ppm after 30min, closing the first alkaline agent dosing pump 10, the backwashing pump 4 and the aeration blower 23, soaking for 2.5h, opening a backwashing pump 4, a first alkaline agent dosing pump 10 and a first alkaline agent flow control device 11, backwashing medicine/water feeding for 30min, soaking for 2.5h, opening an aeration blower 23, aerating for 30min, soaking for 2.5h, opening the backwashing pump 4, the first alkaline agent dosing pump 10 and the first alkaline agent flow control device 11, backwashing medicine/water feeding for 30min, soaking for 2.5h, emptying the reaction chamber 1 after finishing, washing membrane wires with clear water, feeding water, and observing pressure. As shown in FIG. 4, the MBR transmembrane pressure differential gradually increased after the cleaning recovery run, and the transmembrane pressure differential was only 32.9kPa after 144h (6 days) of the run.
Comparative example 1
When the transmembrane pressure difference exceeds 40kPa, emptying the reaction chamber 1, cleaning the MBR hollow fiber membrane 2 in situ by using a high-pressure water gun and a blowing fan, feeding water until membrane filaments are completely immersed, opening a second alkaline agent dosing pump 12 and a second alkaline agent flow control facility 13 to add sodium hypochlorite solution in an alkaline cleaning agent storage tank 9 into the reaction chamber 1 in a multipoint distribution dosing mode, keeping the effective chlorine concentration in the reaction chamber 1 at 3000ppm, soaking for 12 hours, emptying the reaction chamber, washing the membrane filaments by using clear water, feeding water, and observing the pressure. As shown in FIG. 5, the MBR transmembrane pressure difference gradually increased after the recovery cleaning recovery operation, and the transmembrane pressure difference reached 40kPa after 132h (5.5 days) of the operation.
Comparative example 2
When transmembrane pressure difference exceeds 40kPa, emptying the reaction chamber 1, cleaning an MBR hollow fiber membrane 2 in situ by using a high-pressure water gun and a blowing fan, feeding water until membrane filaments are completely immersed, opening a second alkaline agent dosing pump 12 and a second alkaline agent flow control facility 13 to add sodium hypochlorite solution in an alkaline cleaning agent storage tank 9 at a fixed point, keeping 3000ppm of effective chlorine in the reaction chamber 1, opening an aeration blower 23, soaking for 12 hours, aerating in the whole process, emptying the reaction chamber after the completion, washing the membrane filaments by using clear water, feeding water, and observing pressure. As shown in FIG. 6, the MBR transmembrane pressure differential gradually increased after the recovery cleaning recovery run, and the transmembrane pressure differential reached 40kPa after 144h (6 days) of the run.
Comparative example 3
When transmembrane pressure difference exceeds 40kPa, emptying the reaction chamber 1, cleaning an MBR hollow fiber membrane 2 in situ by using a high-pressure water gun and a blowing fan, feeding water until membrane filaments are basically immersed, opening a second alkaline agent feeding pump 12 and a second alkaline agent flow control facility 13 to feed sodium hypochlorite solution in an alkaline agent storage tank 9 into the reaction chamber 1 in a multi-point distribution feeding mode, simultaneously opening a back washing pump 4 and a back washing valve 6, opening a first alkaline agent feeding pump 10 and a first alkaline agent flow control facility 11 to feed sodium hypochlorite solution mixed water in the alkaline agent storage tank 9 into the MBR hollow fiber membrane 2 in a back washing mode, simultaneously opening an aeration blower 23 and a valve 25, closing the second alkaline agent feeding pump 12 after 5min, keeping the effective chlorine concentration of the reaction chamber 1 at 3000ppm after 30min, closing the first alkaline agent feeding pump 10 and the back washing pump 4, continuously aerating and soaking for 12h, emptying the reaction chamber after the operation is finished, and (5) washing the membrane filaments by clear water, feeding water for running, and observing pressure. As shown in FIG. 7, the transmembrane pressure difference of the MBR gradually increased after the cleaning recovery operation, and the transmembrane pressure difference reached 37.5kPa after 144h (6 days) of the operation.
Energy consumption comparison of examples and comparative examples
| Example 1 | Comparative example 1 | Comparative example 2 | Comparative example 3 | |
| Run time (h) | 144 | 132 | 144 | 144 |
| Limiting pressure differential across membrane (kPa) | 32.9 | 40 | 40 | 37.5 |
| Energy consumption (aeration and recoil) | 1/12+1/8 | 0 | 1 | 1+1/24 |
| Medicine consumption | 5/6 | 1 | 1 | 1 |
The above description is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are also within the scope of the present invention. The invention extends to any novel feature or any novel combination of features disclosed in this specification and any novel method or process steps or any novel combination of features disclosed.
Claims (10)
1. A recovery cleaning method for an MBR hollow fiber membrane is characterized by comprising the following steps:
step 1: stopping discharging water from the MBR hollow fiber membrane to be cleaned, emptying the reaction chamber, cleaning a filter cake layer of the MBR hollow fiber membrane, and injecting clear water until membrane filaments are immersed;
step 2: considering the internal and external parts and concentration polarization of the MBR hollow fiber membrane, adding a cleaning agent into the reaction chamber, introducing the cleaning agent/water into the MBR hollow fiber membrane in a back flushing mode, and aerating in the reaction chamber, wherein the concentration of the cleaning agent in the MBR hollow fiber membrane is less than that of the cleaning agent in the reaction chamber; then, stopping adding the cleaning agent into the reaction chamber, but continuously aerating, and continuously introducing the cleaning agent/water into the MBR hollow fiber membrane in a back flushing manner; then stopping aeration of the reaction chamber, stopping introducing cleaning agent/water into the MBR hollow fiber membrane in a back flushing mode, and soaking for 30-180 min;
and step 3: after soaking, introducing cleaning agent/water into the interior of the MBR hollow fiber membrane for backwashing for 20-60 min;
and 4, step 4: after the back flushing is stopped, soaking for 30-180 min;
and 5: after soaking, aerating the reaction chamber for 20-60 min;
and 6: stopping the aeration of the reaction chamber, and soaking for 30-180 min;
and 7: and repeating the steps 3-6.
2. The MBR hollow fiber membrane restorative cleaning method according to claim 1, wherein in the step 1, when the transmembrane pressure difference of the MBR hollow fiber membrane exceeds 40kPa, the effluent water of the MBR hollow fiber membrane to be cleaned is stopped.
3. The MBR hollow fiber membrane restorative cleaning method according to claim 1, wherein the method for cleaning the cake layer of the MBR hollow fiber membrane in the step 1 is at least one of in-situ high-pressure water cleaning, blowing and sweeping of a blower and ex-situ high-pressure water cleaning.
4. The MBR hollow fiber membrane restorative cleaning method according to claim 1, wherein the step 2 comprises two modes of adding a cleaning agent through dispersed pressure holes and introducing the cleaning agent into the MBR membrane in a back washing mode after adjusting the concentration of the cleaning agent in the pipeline through back washing water, so that the adjustment of the concentration of the cleaning agent can be realized in the device, and the concentration of the cleaning agent added through the dispersed pressure holes is higher than that of the cleaning agent adjusted by the back washing water.
5. The MBR hollow fiber membrane restorative cleaning method as set forth in claim 1, wherein the cleaning in the steps 3-6 is in-situ cleaning, the cleaning process is cleaning agent/water back flushing vibration, soaking, aeration, soaking 'water-gas cooperation' process, and the sequence and duration of each stage can be adjusted according to actual conditions.
6. The MBR hollow fiber membrane restorative cleaning method according to claim 4, wherein the cleaning agent in the step 2 is an alkaline cleaning agent or an acid cleaning agent, the cleaning agent in the step 2 is an acid cleaning agent and is an alkaline cleaning process, the cleaning agent in the step 2 is an alkaline cleaning agent and is an alkaline cleaning process, and the MBR hollow fiber membrane restorative cleaning method is applicable to any one of only acid cleaning or only alkaline cleaning, or alkaline cleaning before acid cleaning.
7. The MBR hollow fiber membrane restorative cleaning method as set forth in claim 4 or 5, wherein when the step 2 is an alkaline cleaning agent, the concentration of the alkaline cleaning agent in the reaction chamber is kept at 1500-5000ppm, and the pH is adjusted to 10-12 by using sodium hydroxide.
8. The MBR hollow fiber membrane recovery cleaning method according to claim 4 or 5, wherein when the step 2 is a pickling agent, the concentration of the pickling agent in the reaction chamber is 1.5% -3%wt%。
9. The MBR hollow fiber membrane restorative cleaning method according to claim 6, wherein the alkaline cleaning agent is at least one of sodium chlorate, potassium hypochlorite and hydrogen peroxide.
10. The MBR hollow fiber membrane restorative cleaning method according to claim 6, wherein the acid pickling agent is at least one of citric acid, oxalic acid and oxalic acid.
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