CN105948236A - Integral membrane coagulation reactor (MCR) and water treatment technology - Google Patents
Integral membrane coagulation reactor (MCR) and water treatment technology Download PDFInfo
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- CN105948236A CN105948236A CN201610529503.7A CN201610529503A CN105948236A CN 105948236 A CN105948236 A CN 105948236A CN 201610529503 A CN201610529503 A CN 201610529503A CN 105948236 A CN105948236 A CN 105948236A
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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
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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
- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention provides an integral membrane coagulation reactor (MCR) and a water treatment technology. The integral MCR comprises a membrane pool, and a membrane component and an aerating apparatus which are arranged in the same membrane pool. A coagulant is injected into the membrane pool while aeration is carried out at the bottom of the membrane pool, and the aeration rate is more than or equal to 0.05L/ min, so that the coagulant is evenly dissolved in the membrane pool, and the particle sizes of flocs are enabled to stably increase. The contaminants are effectively removed by the coagulant, so that the transmembrane pressure difference increment caused by the contaminants is slowed down. The water quality of effluent is guaranteed by utilizing the interception performance of an ultrafiltration membrane. Furthermore, the surface of the membrane is not damaged by the flocs in a running process. The flocs are continuously formed in the membrane pool, so that the flocs are large in density, sludge is conveniently discharged, and less sludge is left. The integral MCR and the water treatment technology can reduce the occupied area to a great extent while guaranteeing contaminant removal efficiency and retarding membrane fouling. The integral MCR and the water treatment technology can be used for treating drinking water of a contaminated water source, and are also applied to urban sewage plant treatment and reclaimed water purification.
Description
Technical field
The invention belongs to water process and control membrane fouling technical field, be specifically related to integral type film coagulation reactor (MCR) and water
Process technique.
Background technology
Conventional water treatment process (coagulation-precipitation-filtration-sterilization) applicating history of existing more than 100 year, but along with water pollution and right
The continuous lifting of water quality requirement, common process increasingly shows inadaptability.When people pay high attention to water quality health risk problem
And when making great efforts to tackle its technological challenge brought, new principle, new method and the new technology that water quality safety ensures is just in the problem of solution
Actual demand in there is positive change.In the process, people using new diseases as break through emphasis, it is intended to
For improving tradition water treatment technology offer scientific method and Technology in most basic means.To this end, embrane method purifies reason in recent years
Opinion and application have become the study hotspot of this area, and membrane technology is also widely used for actual engineering of water treatment.
Although membrane technology water process in application more prevalent, but fouling membrane the most all be reduce film cleaning water bottleneck because of
Element.In order to effectively slow down and control fouling membrane, before film processing system, generally carry out a certain degree of coagulation pretreatment.By
At present, two kinds of coagulation dual-membrane process have been explored: (1) conventional film group technology, coagulation process the most in advance.Film processing system
Before have coagulation and precipitation unit.Pollutant first with coagulant coagulation, after precipitation unit enter film processing system；(2) direct
Filter membrane group technology, i.e. abbreviated system.Without precipitation unit before film processing system.Pollutant are directly entered at film after coagulation
Reason system.
Containing coagulation and two processing units of precipitation in conventional film group technology, floor space is bigger.On the other hand, in sedimentation tank
Sludge density is relatively small so that sludge volume is bigger.Simultaneously as the existence of precipitation unit, under granule bigger after coagulation is easy
Heavy, less granule is then directly entered film processing system, causes the probability of absorption/blocking fenestra to increase, easily causes serious
Fouling membrane.
For direct filter membrane group technology, owing to without precipitation unit, comparing conventional film group technology, floor space is less.
Being directly entered film processing system after pollutant coagulation, granule is relatively big, is difficult to absorption/blocking fenestra, and fouling membrane degree is relatively light,
But membrane cisterna endoparticle easily precipitates, cause sludge volume and spoil disposal frequency bigger.
Patent application CN101279805A discloses " embrane method drinking water treatment process and equipment ", a kind of embrane method potable water
Reason equipment, including: pretreatment unit, coagulating basin, membrance separation pond；Pretreatment unit arranges coarse rack and Y-piece road filters
Devices etc., carry out pretreatment to former water, in case former impurities in water blocking intake pump and water inlet meter；Coagulating basin is Mechanical coagulation pond,
Former water is carried out coagulation；Membrance separation pond, uses curtain type film assembly structure, filters former water.
Patent application CN 103566762 A open " a kind of immersion ultrafiltration system ", coagulant dosage is intake at submerged ultrafiltration
The water sucking mouth of pump, the former water of dosing coagulant filters in entering immersed ultrafiltration membrane pond.Use In-line coagulation and immersion
The group technology of ultrafilter membrane, ultrafilter membrane backwashing water is back in raw water tubes road simultaneously, carries out reuse.And immersion ultrafiltration system
It is provided with mud drainage slot bottom system, can periodically discharge mud, it is ensured that the stable operation of immersion ultrafiltration.
On the basis of ensureing contaminant removal efficiency, for reducing floor space and spoil disposal further, the present invention uses and is filled by coagulation
Put with immersion type membrane component be placed in same membrane cisterna integral type film coagulation reactor (Membrane Coagulation Reactor,
MCR).By aeration bottom membrane cisterna so that coagulation uniformly and persistently forms flco.Utilize coagulation, be especially formed in situ
Flco, efficiently remove pollutant, utilize simultaneously membrane module crown_interception ensure effluent quality.With conventional film group technology and
Directly filter membrane group technology is compared, and integral type film coagulation process not only floor space reduces further, and can make full use of mixed
It is formed in situ the high efficiency of flco after Ning, preferably removes pollutant and slow down the pollution of ultrafilter membrane.Additionally, the mud formed
Density is relatively big, and spoil disposal is convenient and mud amount is less.
Summary of the invention
It is an object of the invention to provide a kind of water that can effectively reduce floor space, operational management convenience and can efficiently remove pollutant
Process process and integral type film coagulation reactor (Membrane Coagulation Reactor, MCR).
For achieving the above object, the present invention takes below scheme:
A kind of integral type film coagulation reactor (MCR), including: membrane cisterna, and it is arranged at the membrane module in same membrane cisterna and exposure
Device of air；Membrane cisterna is connected with coagulant dosage pond by pipeline in-line pumping pump；Mud valve it is additionally provided with bottom membrane cisterna；Reaction
Device is additionally provided with membrane cisterna outlet.
Present invention achieves coagulation process integrated with membrane process, while ensureing contaminant removal efficiency, significantly reduce
Floor space.
Further, according to the demand of membrane treatment process, described membrane module is connected with pressure vacuum gauge also by pipeline.
Further, described aerator is arranged at the bottom in membrane cisterna, distance top membrane module 10～50cm.
Further, described aerator is boring aeration pipe or aeration head, and the level interval of aeration tube or aeration head is 5～50
Cm, aeration tube or aeration head take high level when being relatively large in diameter.
Further, the aeration rate >=0.05L/min of described aerator, fouling membrane degree takes high level time serious.
Further, described membrane module is low-pressure membrane assembly, and its form is immersion, including micro-filtration membrane or ultrafilter membrane, and end
End is free end, to facilitate spoil disposal.
It is as follows that the present invention also provides for a kind of integral type film coagulation water treatment technology:
Utilize above-mentioned integral type film coagulation reactor, coagulant dosage pond configures finite concentration coagulant, exposes bottom membrane cisterna
In the case of gas, by suction pump, coagulant persistently being pumped into membrane cisterna, pending water is directly injected into membrane cisterna, same stepping in membrane cisterna
Row coagulation and film process, and the water after process is discharged through membrane cisterna outlet；For ensureing treatment effect, pending water stops in membrane cisterna
Time palpus >=10min.Physical property backwashing time is 20～30min, backwashing water speed 2 times water inlet speed.Maintainability
Cleaning frequency is 5～10 days/time.When the 60～70% of flux depression to initial film flux, membrane module must be carried out chemistry clear
Wash.
Further, described coagulant is inorganic coagulant, and its kind is preferably aluminum salt, iron salt coagulant or ferro-aluminum
Compound coagulant.
Further, the water level processed in technique in membrane cisterna exceeds membrane module 100～200cm.
Further, the spoil disposal frequency of described technique is 5～15 days/time.Every time during spoil disposal, stop aeration, after standing 30min
Spoil disposal, water level decreasing is to membrane module.
Present invention have the advantage that
1, utilize aeration bottom membrane cisterna to reach the purpose of coagulation, give full play to be formed in situ the activity of flco, efficiently remove pollutant.
2, in utilizing membrane cisterna, flco is persistently formed, the feature that membrane cisterna endoparticle thing density is bigger, facilitates spoil disposal and mud amount less.
3, floor space is little, producing water ratio is high and the loss of flood peak is little, is suitable for old fish drugs and new waterworks construction.Operating cost is low
Honest and clean, and operational management is convenient.
Accompanying drawing explanation
Fig. 1: integral type film coagulation reactor schematic diagram of the present invention；
Wherein, 1-membrane cisterna, 2-membrane module, 3-aerator, 4-suction pump, 5-coagulant dosage pond, 6-pressure vacuum gauge, 7-
Membrane cisterna outlet, 8-mud valve.
Detailed description of the invention
Below by specific embodiment, and combine accompanying drawing, be further discussed below the present invention.Unless stated otherwise, embodiment
Middle techniques not described means all can realize by mode known in those skilled in the art.It addition, embodiment is interpreted as
Illustrative, and unrestricted the scope of the present invention, the spirit and scope of the invention are limited only by the claims that follow.For ability
For field technique personnel, on the premise of without departing substantially from spirit and scope of the present invention, to the material component in these embodiments, use
Various amendments that amount, size, shape are carried out, replace, improve and fall within protection scope of the present invention, and the present invention is limited
Design parameter should have admissible range of error.
In order to be more fully understood that the present invention, main portions or parts to relating in figure are numbered.It is identically numbered expression phase
With or similar position or parts, there is essentially identical function, but its size concrete in difference figure or embodiment, shape,
Structure is the most identical.
Embodiment 1
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use routine mixed
Solidifying membrane treatment process (comprising independent coagulation unit, precipitation unit and the conventional equipment of film processing unit).Persistently add aluminium salt to mix
Solidifying agent, 5mg/L every day in terms of aluminum.Wherein, mechanical agitation is fast turn of (200rpm) 1min, slow-speed (50rpm) 15min.
Raw water pump is entered coagulating basin, with 1m after sedimentation tank3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.By heavy
Pond, shallow lake spoil disposal, wherein spoil disposal frequency is 3 days/time.After running 30 days continuously, transmembrane pressure increases to 48kPa, water outlet DOC removal
Rate is 79%.
Embodiment 2
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use short route
Technique (comprises independent coagulation unit and the conventional equipment of film processing unit).Persistently add aluminum salt, every day 5 in terms of aluminum
mg/L.Wherein, mechanical agitation is fast turn of (200rpm) 1min, slow-speed (50rpm) 15min.Raw water pump is entered coagulating basin,
And with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Running 30 days continuously, spoil disposal frequency is 3 days/time.
Stand 30min every time during spoil disposal, open mud valve bottom membrane cisterna and discharge half deposit.After running 30 days continuously, transmembrane pressure increases
To 42kPa, water outlet DOC clearance is 81%.
Embodiment 3
With reference to shown in Fig. 1, in one exemplary embodiment of the present invention, a kind of integral type film coagulation reactor, including: film
Pond 1, the membrane module 2 being arranged in same membrane cisterna and aerator 3；Membrane cisterna 1 is thrown with coagulant by pipeline in-line pumping pump 4
Add pond 5 to be connected.Membrane module 2 is connected with pressure vacuum gauge 6 also by pipeline.Reactor is additionally provided with membrane cisterna outlet 7.
Mud valve 8 it is additionally provided with bottom membrane cisterna 1.
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use the present invention
Integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt, film group in coagulant dosage pond 5
Part 2 and aerator 3 are placed in same membrane cisterna 1.
By suction pump 4, aluminum salt is persistently injected in membrane cisterna 1,5mg/L every day in terms of aluminum.Wherein, aeration rate is 0.05
L/min.Running 30 days continuously, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge
Half deposit.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Fortune continuously
Row after 30 days transmembrane pressure increase to 38kPa, water outlet DOC clearance is 86%.
Embodiment 4
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use this
Bright integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing iron salt coagulant, film in coagulant dosage pond 5
Assembly 2 and aerator 3 are placed in same membrane cisterna 1.
Iron salt coagulant is persistently injected in membrane cisterna 1,5mg/L every day in terms of ferrum.Wherein, aeration rate is 0.05L/min.Even
Reforwarding row 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposition
Thing.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Run 30 days continuously
Rear transmembrane pressure increases to 39kPa, and water outlet DOC clearance is 84%.
Embodiment 5
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use the present invention
Integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt, film group in coagulant dosage pond 5
Part 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,5mg/L every day in terms of aluminum.Wherein, aeration rate is 0.1L/min.Continuously
Running 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposit.
Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.After running 30 days continuously across
Mould difference increases to 36kPa, and water outlet DOC clearance is 85%.
Embodiment 6
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 2～10mg/L in pending water.Use the present invention
Integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt, film group in coagulant dosage pond 5
Part 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,5mg/L every day in terms of aluminum.Wherein, aeration rate is 0.5L/min.Continuously
Running 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposit.
Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.After running 30 days continuously across
Mould difference increases to 31kPa, and water outlet DOC clearance is 82%.
Embodiment 7
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 10～25mg/L in pending water.Use this
Bright integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt, film in coagulant dosage pond 5
Assembly 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,10mg/L every day in terms of aluminum.Wherein, aeration rate is 0.05L/min.Even
Reforwarding row 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposition
Thing.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Run 30 days continuously
Rear transmembrane pressure increases to 33kPa, and water outlet DOC clearance is 87%.
Embodiment 8
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 20～50mg/L in pending water.Use this
Bright integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt, film in coagulant dosage pond 5
Assembly 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,20mg/L every day in terms of aluminum.Wherein, aeration rate is 0.05L/min.Even
Reforwarding row 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposition
Thing.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Run 30 days continuously
Rear transmembrane pressure increases to 27kPa, and water outlet DOC clearance is 92%.
Embodiment 9
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 100～200mg/L in pending water.Use this
Invention integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt in coagulant dosage pond 5,
Membrane module 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,30mg/L every day in terms of aluminum.Wherein, aeration rate is 0.05L/min.Even
Reforwarding row 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposition
Thing.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Run 30 days continuously
Rear transmembrane pressure increases to 37kPa, and water outlet DOC clearance is 88%.
Embodiment 10
The present embodiment is original sub-block, dissolved organic carbon (DOC) content 200～500mg/L in pending water.Use this
Invention integral type film coagulation reactor and water treatment technology, as it is shown in figure 1, containing aluminum salt in coagulant dosage pond 5,
Membrane module 2 and aerator 3 are placed in same membrane cisterna 1.
Aluminum salt is persistently injected in membrane cisterna 1,50mg/L every day in terms of aluminum.Wherein, aeration rate is 0.05L/min.Even
Reforwarding row 30 days, spoil disposal frequency is 10 days/time.Stand 30min every time during spoil disposal, open mud valve 8, discharge half deposition
Thing.Raw water pump is entered membrane cisterna, and with 1m3/ h enters membrane cisterna, and in membrane cisterna, hydraulic detention time is 0.5h.Run 30 days continuously
Rear transmembrane pressure increases to 41kPa, and water outlet DOC clearance is 93%.
Claims (10)
1. an integral type film coagulation reactor, including: membrane cisterna, and it is arranged at the membrane module in same membrane cisterna and aerator；
Membrane cisterna is connected with coagulant dosage pond by pipeline in-line pumping pump；Mud valve it is additionally provided with bottom membrane cisterna；Described reaction
Device is additionally provided with membrane cisterna outlet.
2. a kind of integral type film coagulation reactor as claimed in claim 1, it is characterised in that described aerator is arranged at membrane cisterna
Interior bottom, distance top membrane module 10～50cm.
3. a kind of integral type film coagulation reactor as claimed in claim 1, it is characterised in that described aerator is boring aeration
Manage or aeration head, and the level interval of aeration tube or aeration head is 5～50cm.
4. a kind of integral type film coagulation reactor as claimed in claim 1, it is characterised in that the aeration rate of described aerator >=
0.05L/min。
5. a kind of integral type film coagulation reactor as claimed in claim 1, it is characterised in that described membrane module is low-pressure membrane group
Part, its form is immersion, and end is free end.
6. integral type film coagulation reactor as claimed in claim 1 a kind of, it is characterised in that described membrane module also by pipeline with
Pressure vacuum gauge is connected.
7. an integral type film coagulation water processes membrane process method, it is characterised in that utilize the arbitrary described integral type of claim 1-6
Film coagulation reactor, configures finite concentration coagulant in coagulant dosage pond, bottom membrane cisterna in the case of aeration, logical
Crossing suction pump and coagulant persistently pumps into membrane cisterna, pending water is directly injected into membrane cisterna, synchronizes to carry out coagulation and film in membrane cisterna
Filtering, the water after filtration is discharged through membrane cisterna outlet；For ensureing treatment effect, pending water time of staying palpus in membrane cisterna
≥10min；When the 60～70% of flux depression to initial film flux, membrane module must be carried out Chemical cleaning.
8. integral type film coagulation water treatment technology as claimed in claim 7, it is characterised in that described coagulant is inorganic
Coagulant, its kind is aluminum salt, iron salt coagulant or ferroaluminium composite coagulant.
9. integral type film coagulation water treatment technology as claimed in claim 7, it is characterised in that membrane cisterna in described process technique
Interior water level exceeds membrane module 100～200cm.
10. integral type film coagulation water treatment technology as claimed in claim 7, it is characterised in that the spoil disposal frequency of described technique
It it is 5～15 days/time；Every time during spoil disposal, stopping aeration, stand spoil disposal after 30min, water level decreasing is to membrane module.
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| CN108706686A (en) * | 2018-05-29 | 2018-10-26 | 苏州膜海分离技术有限公司 | Batch-type flocculation-hyperfiltration treatment technique of micro-polluted water |
| CN108658297A (en) * | 2018-06-04 | 2018-10-16 | 南通大学 | A kind of low-pressure membrane water technology based on fluid bed MCR |
| CN110655244A (en) * | 2019-10-22 | 2020-01-07 | 广东广深环保科技有限公司 | MCR membrane chemical separation device |
| CN111302517A (en) * | 2020-02-27 | 2020-06-19 | 中国科学院生态环境研究中心 | Device and method for retarding membrane pollution |
| CN113816464A (en) * | 2021-10-09 | 2021-12-21 | 中车唐山机车车辆有限公司 | Water treatment method and device for reducing membrane pollution |
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Application publication date: 20160921 |