CN1548219A - Operation method of externally pressurized hollow fiber membrane separator - Google Patents
Operation method of externally pressurized hollow fiber membrane separator Download PDFInfo
- Publication number
- CN1548219A CN1548219A CNA031311377A CN03131137A CN1548219A CN 1548219 A CN1548219 A CN 1548219A CN A031311377 A CNA031311377 A CN A031311377A CN 03131137 A CN03131137 A CN 03131137A CN 1548219 A CN1548219 A CN 1548219A
- Authority
- CN
- China
- Prior art keywords
- hollow fiber
- operation method
- separation device
- fiber membrane
- backwash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The first operation process in hollow fiber membrane separator system includes: work state; air and water double-washing state including introducing small amount of original liquid to wash the membrane in the right direction while introducing compressed air to wash the membrane in the right direction; and draining state. The second operation process includes: work state; air and water double-washing state including introducing small amount of original liquid to wash the membrane in the right direction while introducing compressed air to wash the membrane in the right direction; inverse washing state with inverse washing liquid; and draining state. The third operation process includes: work state; air and water double-washing state including introducing small amount of original liquid with chemical added to wash the membrane in the right direction while introducing compressed air to wash the membrane in the right direction; and draining state.
Description
Technical field
The present invention relates to a kind of membrane separation technique, relate in particular to a kind of operation method of external pressure hollow fiber membrane separation device.
Background technology
Along with the raising of people's living standard, people improve constantly the requirement of drinking water, so-called pure water, space water or purify waste water and enter daily life.And, produce and water for industrial use, require also more and more higher as fields such as biochemistry, medicine, food, condiment to the water purification degree.The micro-filtration developed of people and the ultrafiltration membrane technique purification that is used for water quality in recent years, positive adaptation this needs, and obtained good actual effect.Wherein make with the most use with the external pressure hollow-fibre membrane especially.This is because external pressure hollow-fibre membrane (hereinafter to be referred as film) has the area maximum of filling film in the unit volume, can remove the algae in the former water, multiple suspensions such as microorganism and colloidal substance, and purify the purity advantages of higher.But in actual applications, the inner chamber of film, hole and outer wall be owing to the delay of various suspensions, the water flux that alluvial makes film descend rapidly, even obstruction and cisco unity malfunction.Therefore the cleaning to film is the indispensable important component part of film application technology.
The applicant with regard to the application of film cleaning technique many patents, wherein one is " external pressure hollow fiber membrane separation device and using method thereof " (publication number is CN1333080A).This application has mainly been made important improvement at the structure and the flow route design aspect of membrane module, has solved the online efficient cleaning problem of film well.But it still exists deficiency: the design of the exterior line of membrane module is not perfect in this film device.Other one be " hollow fiber membrane separation device and using method thereof " (CN1347752A).This application has mainly been carried out perfect to the exterior line design of membrane module in the film device, designed chemical cleaning circuit and backwash loop.
Disclosed cleaning method is in CN1347752A: the first cleaning state: compressed air and water clean membrane module simultaneously, carry out promptly also that air water is two to be washed.At above-mentioned cleaning state, gas is just washed, and the water backwash adds chemicalses such as oxidant as required.The second cleaning state: a large amount of backwash liquors clean film.
The shortcoming that above-mentioned cleaning exists is: pipeline is many, the operation complexity.
In addition, former technology is the backwash dosing, because medicament itself is unholiness, and the filtered solution side of polluted membrane, thereby influence product water water quality, and be difficult to medicament itself is carried out purified treatment.
Summary of the invention
The objective of the invention is provides the membrane separation device that a kind of operation is simple, cleaning performance is good operation method in order to solve the problem of above-mentioned proposition.
Another object of the present invention is: a kind of hollow fiber membrane separation device operation method that filtered solution is not polluted is provided.
In order to realize the foregoing invention purpose, the invention provides the operation method of a kind of hollow fiber membrane separation device system, comprising: duty; The two states of washing of air water: a small amount of stoste is introduced membrane module, film is just washed, introduce compressed air simultaneously film is just washed.
The operation method of second kind of hollow fiber membrane separation device system provided by the invention comprises: duty; The two states of washing of air water: a small amount of stoste is introduced membrane module, film is just washed, introduce compressed air simultaneously film is just washed.Backwash state: backwash liquor is introduced membrane module, film is carried out backwash.
The operation method of the third hollow fiber membrane separation device system provided by the invention comprises: duty; The two states of washing of air water: a small amount of stoste is introduced membrane module, and before stoste entered membrane module, dosing in stoste was just washed film, introduces compressed air simultaneously film is just washed.Backwash state: backwash liquor is introduced membrane module, film is carried out backwash.
Operation method by external pressure hollow membrane assembly provided by the invention can be achieved as follows effect:
1, operation is simple, and cleaning performance is good;
2, save backwash liquor;
3, can prevent the filtered solution side of polluted membrane because medicament itself is unholiness, water water quality is produced in influence;
4, because the organic matter on the oxidisability medicament that adds energy sterilization and removal film surface; The inorganic matter on the antisludging agent energy membrane removal surface that adds by the acting in conjunction of two class medicaments, is effectively restored membrane flux.
Description of drawings
Fig. 1 is the overall structure schematic diagram of first embodiment of the invention;
Fig. 2 is the overall structure schematic diagram of second embodiment of the invention;
Fig. 3 is the overall structure schematic diagram of third embodiment of the invention;
Fig. 4 is the schematic diagram that the present invention controls another embodiment of stock solution flow when cleaning.
The specific embodiment
Be described in further detail the present invention below in conjunction with drawings and Examples.
Be provided with a plurality of valves in the device of the present invention, the switching by by-pass valve control is controlled the operation of membrane module and cleaning, blowdown.If valve in the accompanying drawing according to type, can be divided into hand-operated valve, automatic valve (can be pneumatic or electronic diaphragm valve, butterfly valve, ball valve).
If divide according to function or effect, valve 1,1a are import pressure regulator valve or control valve; Valve 11,11a are called the import automatic valve; Valve 2 is outlet pressure regulator valve or control valve; Valve 19 is called the outlet automatic valve; Valve the 4, the 5th, transfer valve is used for the conversion between film mask work and the Chemical cleaning work; Valve 6 is working barrel imported valves; Valve the 8, the 9th, the low level drain valve.Valve 3 is backwash control valve, the flow size that is used to regulate backwash liquor; Valve 15 is called the backwash automatic valve; Valve 7 is called the backwashing pump inlet valve; Valve 12 is called the cleaning air bleeding valve; Valve 13 is called the cleaning drain valve; Valve 14 is called the filtered solution outlet valve; Valve 17 is called intake valve; Valve 18 is called the dosing check valve.
P1, P2, P3 are Pressure gauge in the accompanying drawing, and F1 is flowmeter or flow sensor.
Below with reference to Fig. 1 first embodiment of the invention membrane separation device operation method is elaborated.
As shown in Figure 1, in the membrane module separator of the present invention's design, membrane module 21 pipes are connected to many pipelines.The pipeline that its direct pipe connects has: liquid flows into pipeline 40, and liquid flows out pipeline 41, circulating reflux pipeline 22, blowoff line 45,46, air supply line 47 etc.Liquid flows out on the pipeline 41 also, and pipe is connected to Chemical cleaning return line 30 and liquid feed line 42.Describe the annexation of each pipeline and membrane module below in detail.
Wherein, aforesaid liquid flows into pipeline 40 pipes and is connected between the lower port 20 of circulating water chennel 28 and membrane module 21, is used for providing liquid to membrane module.Aforesaid liquid flows into pipeline 40 and is provided with parts such as working barrel import manually-operated gate 6, working barrel 29, former water liquid measure control device.
Liquid flows out the pipeline pipe and connects an end pipe of 41 and be connected on the upper port 23 of junctional membrane assembly 21, is used for from the terminal liquid of discharging of membrane module; The other end of liquid outflow pipeline connects two branch roads, and a branch road is a liquid feed line 42, and aforesaid liquid supply line 42 is connected with product water tank 25, is used for and will be sent to generation tank 25 through the filtered solution after the membrane module filtration under the duty.The another one branch road is a Chemical cleaning return line 30, and above-mentioned Chemical cleaning return line 30 is connected with circulating water chennel 28, is used for when membrane module carries out Chemical cleaning after longer a period of time of operation the cleaning fluid that contains chemicals being circulated.Above-mentioned Chemical cleaning return line 30 is provided with the switch valve 5 that is used to switch, and aforesaid liquid supply line 42 is provided with by manual switchover valve 4.Usually move at membrane module, valve 5 is closed when cleaning, valve 4 opens.Have only after membrane module moved for 1～5 week, when membrane module is carried out Chemical cleaning, just open valve 5, valve-off 4.
Circulating reflux pipeline 22 pipes are connected between the upside mouth 16 and circulating water chennel 28 of membrane module 21, this circulating reflux pipeline 22 is provided with autocontrol valve 19 and hand control valve 2 and Pressure gauge, hand control valve and Pressure gauge all are regulating system pressure, water yields when system's initial launch, after entering automatic control, only control by automatic valve.
On the lower port 20 of membrane module 21 also pipe be connected to and be used to supply compressed-air actuated air supply line 47, compressed air is supplied air at the cleaning state to membrane module from the control of air reservoir (not shown) by gas flowmeter, valve.
In the present invention, a kind of embodiment of the former water liquid measure control device that is provided with on the liquid inflow pipeline 40 is that dual-inlet pipeline 44 is set.As shown in Figure 1, dual-inlet pipeline 44 comprises first inlet pipeline that is provided with valve 1,11 and second inlet pipeline that is provided with valve 1a and 11a.The effect of above-mentioned dual-inlet pipeline 44 is: two inlet pipelines are all opened during work, wash under the state in that air water is two, close automatic valve 11 closing first inlet pipeline, thereby realize inflow is reduced to 1/20 to 1/2 of working flow.
In addition, can as shown in Figure 4 dual-inlet pipeline be set yet, change VFC into,, can control under the two cleaning states of washing of air water yet and make a small amount of former water enter membrane module by the output of Frequency Converter Control raw water pump 29.
Describe the operating procedure of first embodiment of the invention membrane separation device system below in detail.
Adopt the present invention's membrane separation device as shown in Figure 1, move by following processing step:
1) duty:
Connect liquid and flow into pipeline 40, liquid outflow pipeline 41, liquid feed line 42, circulating reflux pipeline 22, other pipelines are closed.Former water in the circulating water chennel 28 flows into pipeline 40 by liquid and enters into membrane module 21 under the effect of working barrel 29.By the filtration of membrane module, filtered solution flows out from the upper port 23 of membrane module, enters into by liquid outflow pipeline 41, liquid feed line 42 and produces tank 25.Phegma is back to circulating water chennel by circulating reflux pipeline 22.Working time is 10-120 minute, is preferably 10～60 minutes.
2) the two states of washing of air water:
The pipeline that closing liquid flows out pipeline 41 and is connected in its back, blow-off pipe 45 in the connection, and by the control or the VFC of dual-inlet pipeline 44, making the former current output in the circulating water chennel 28 is 1/20 to 1/2 under the normal operating conditions.A small amount of former water enters 21 pairs of films of membrane module and cleans, and simultaneously, compressed air enters into 21 pairs of membrane modules by air supply line 47 to carry out air and just wash.Scavenging period is 10-60 second.
3) blowdown state:
Make liquid stop to flow into pipeline 40 and enter membrane module, connect upper and lower blow-off pipe 45,46, sewage in the membrane module is discharged by liquid.Time is 0～60 second.
4) get back to duty
According to actual conditions, after membrane module moved for 1～5 week, membrane module is carried out Chemical cleaning.
Below with reference to Fig. 2 the second embodiment of the invention membrane separation device is elaborated.
As shown in Figure 2, different with the first embodiment membrane separation device is to have increased backwash pipeline 43.The terminal pipe that backwash pipeline 43 is arranged on aforesaid liquid outflow pipeline 41 connects on two branch roads position in the past, above-mentioned backwash pipeline 43 1 ends and liquid flow out pipeline 41 pipes and connect, the other end carries out pipe with product water tank 25 and connects, and pipeline is provided with backwashing pump 24, backwash control valve 3,15.The backwash pipeline is used at the second cleaning state to membrane module 21 supply backwash liquors.
Describe the operating procedure of second embodiment of the invention membrane separation device system below in detail.
Adopt the present invention's membrane separation device as shown in Figure 2, move by following processing step:
1) duty:
Identical with embodiment 1, the working time is 10-60 minute.
2) the two states of washing of air water:
Identical with embodiment 1, scavenging period is 10-60 second.
3) backwash state:
Connect backwash pipeline 43, liquid outflow pipeline 41, blowoff line 45,46, close other pipelines.The backwash liquor that produces in the water tank 25 enters into membrane module 21 through the part of backwash pipeline 43, liquid outflow pipeline 41 under the effect of backwashing pump 24, membrane module is cleaned.Carry out blowdown by first blowoff line 45, second blowoff line 46.The backwash time is 10-60 second.
4) blowdown state:
Make liquid stop to flow into pipeline 40 and enter membrane module, connect upper and lower blow-off pipe 45,46, sewage in the membrane module is discharged by liquid.Time is 0～60 second.
5) get back to duty
Below with reference to Fig. 3 the third embodiment of the invention membrane separation device is elaborated.
As shown in Figure 3, different with the second embodiment membrane separation device is, flows on the pipeline 40 at liquid dosing valve 18 is set, and is used for when the two cleaning state of washing of air water dosing among the Xiang Yuanshui.This is arranged on the backwash pipeline with prior art dosing valve or liquid flows out on the pipeline obviously different.The dosing valve of prior art is by the dosing in backwash liquor of dosing valve at air water is two washes (gas is just washed, water backwash) cleaning state.The improved benefit of the present invention is: filtered solution side that can the polluted membrane assembly does not influence generation water quality.
Aforesaid liquid stream correspondingly is provided with two dosing valves as two dosing mouths can be set on the pipeline, according to the raw water quality situation, can add oxidisability medicament and antisludging agent respectively or simultaneously under the two cleaning states of washing of air water.Above-mentioned oxidisability medicament can be as chemicals such as clorox, ozone, chlorine dioxide; Above-mentioned antisludging agent can be as chemicals such as commodity antisludging agent, hydrochloric acid.
Describe the operating procedure of third embodiment of the invention membrane separation device system below in detail.
Adopt the present invention's membrane separation device as shown in Figure 3, move by following processing step:
1) duty:
State is identical with embodiment 1, and the working time is 10-60 minute.
2) the two states of washing of air water:
When a small amount of former water in the circulating water chennel 28 passed through the dosing valve, chemicals entered into former water.Can add oxidisability medicament and/or antisludging agent according to the water quality of former water, other are identical with embodiment 1, and scavenging period is 10-60 second.
3) backwash state:
Identical with embodiment 2, the backwash time is 10-60 second.
4) blowdown state:
Make liquid stop to flow into pipeline 40 and enter membrane module, connect upper and lower blow-off pipe 45,46, sewage in the membrane module is discharged by liquid.Time is 0～60 second.
5) get back to duty.
Claims (14)
1, the operation method of a kind of hollow fiber membrane separation device system comprises:
Duty;
The two states of washing of air water: a small amount of stoste is introduced membrane module, film is just washed, introduce compressed air simultaneously film is just washed;
The blowdown state.
2, the operation method of a kind of hollow fiber membrane separation device system comprises:
Duty;
The two states of washing of air water: a small amount of stoste is introduced membrane module, film is just washed, introduce compressed air simultaneously film is just washed;
Backwash state: backwash liquor is introduced membrane module, film is carried out backwash;
The blowdown state.
3, the operation method of a kind of hollow fiber membrane separation device system comprises:
Duty;
The two states of washing of air water: a small amount of stoste is introduced membrane module, and before stoste entered membrane module, dosing in stoste was just washed film, introduces compressed air simultaneously film is just washed;
Backwash state: backwash liquor is introduced membrane module, film is carried out backwash.
The blowdown state.
4, according to the operation method of claim 1,2,3 described hollow fiber membrane separation device systems, it is characterized in that:
Under the duty, the former water in the circulating water chennel (28) flows into pipeline (40) by liquid and enters into membrane module (21) under the effect of working barrel (29); By the filtration of membrane module, filtered solution flows out from the upper port (23) of membrane module, enters into by liquid outflow pipeline (41), liquid feed line (42) and produces tank (25); Phegma is back in the circulating water chennel by circulating reflux pipeline (22).
5, according to the operation method of claim 1,2,3 described hollow fiber membrane separation device systems, it is characterized in that: the following working time of duty is 10-60 minute.
6, according to the operation method of claim 1,2,3 described hollow fiber membrane separation device systems, it is characterized in that:
Air water is two to be washed under the state, and by the control of stock solution flow control device, making the former current output in the circulating water chennel (28) is 1/20 to 1/2 under the normal operating conditions.
7, the operation method of hollow fiber membrane separation device according to claim 6 system is characterized in that:
Clean 10-60 second.
8, the operation method of hollow fiber membrane separation device according to claim 6 system is characterized in that:
The stock solution flow control device is a dual-inlet pipeline.
9, the operation method of hollow fiber membrane separation device according to claim 8 system is characterized in that:
The stock solution flow control device is by the pump variable frequency device, realizes reducing inflow.
10, according to the operation method of claim 2,3 described hollow fiber membrane separation device systems, it is characterized in that:
Under the backwash state, connect backwash pipeline (43), liquid outflow pipeline (41), blowoff line (45,46), the backwash liquor that produces in the water tank (25) enters into membrane module (21) through the part of backwash pipeline (43), liquid outflow pipeline (41) under the effect of backwashing pump (24), membrane module is cleaned.
11, the operation method of hollow fiber membrane separation device according to claim 10 system is characterized in that:
The backwash time is 10-60 second
12, the operation method of hollow fiber membrane separation device according to claim 3 system is characterized in that:
Flow into pipeline (40) at liquid the dosing check valve is set, be used under air water cleaning state, controlling to former water dosing.
13, according to the operation method of claim 3 or 9 described hollow fiber membrane separation device systems, it is characterized in that:
Add oxidisability medicament and/or antisludging agent respectively according to raw water quality; Above-mentioned oxidisability medicament can be as chemicals such as clorox, ozone, chlorine dioxide; Above-mentioned antisludging agent can be as chemicals such as commodity antisludging agent, hydrochloric acid.
14, according to the operation method of claim 1,2,3 described hollow fiber membrane separation device systems, it is characterized in that:
The blowdown state time is 0-60 second.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA031311377A CN1548219A (en) | 2003-05-13 | 2003-05-13 | Operation method of externally pressurized hollow fiber membrane separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA031311377A CN1548219A (en) | 2003-05-13 | 2003-05-13 | Operation method of externally pressurized hollow fiber membrane separator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1548219A true CN1548219A (en) | 2004-11-24 |
Family
ID=34322801
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA031311377A Pending CN1548219A (en) | 2003-05-13 | 2003-05-13 | Operation method of externally pressurized hollow fiber membrane separator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1548219A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100548451C (en) * | 2004-12-24 | 2009-10-14 | 西门子水技术公司 | Cleaning in the membrane filtration system |
| WO2009143740A1 (en) * | 2008-05-30 | 2009-12-03 | 北京汉青天朗水处理科技有限公司 | Method and apparatus for cleaning a film seperating device |
| CN101391819B (en) * | 2007-09-18 | 2011-06-01 | 旭化成化学株式会社 | Drinking water filtering system |
| CN102463035A (en) * | 2010-11-02 | 2012-05-23 | 赛普特环保技术(厦门)有限公司 | Coiled membrane separating technology and equipment with forward feeding and reversed washing processes |
| CN102485329A (en) * | 2011-03-22 | 2012-06-06 | 绵阳美能材料科技有限公司 | External-compression hollow fiber membrane cleaning method with no backwashing process |
| CN103232092A (en) * | 2013-05-09 | 2013-08-07 | 天津膜天膜科技股份有限公司 | Method for realizing water treatment by using pressure type continuous membrane filtering system |
| CN106823820A (en) * | 2017-03-03 | 2017-06-13 | 同济大学 | A kind of integrated apparatus for obtaining metal film operation and cleaning duty parameter |
| CN112717696A (en) * | 2020-12-16 | 2021-04-30 | 艾克飞膜材(嘉兴)有限公司 | Ultrafiltration membrane system cleaned by micro-bubble ozone and cleaning method thereof |
| CN113226523A (en) * | 2018-12-27 | 2021-08-06 | 株式会社久保田 | Ultrafiltration device and method for cleaning ultrafiltration device |
| CN114275844A (en) * | 2021-11-25 | 2022-04-05 | 上海市政工程设计研究总院（集团）有限公司 | Container immersed membrane filtering device and flushing control method thereof |
-
2003
- 2003-05-13 CN CNA031311377A patent/CN1548219A/en active Pending
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100548451C (en) * | 2004-12-24 | 2009-10-14 | 西门子水技术公司 | Cleaning in the membrane filtration system |
| CN101391819B (en) * | 2007-09-18 | 2011-06-01 | 旭化成化学株式会社 | Drinking water filtering system |
| US9028622B2 (en) * | 2008-05-30 | 2015-05-12 | Beijing Ecojoy Water Technology Co., Ltd. | Method and apparatus for cleaning a film seperating device |
| WO2009143740A1 (en) * | 2008-05-30 | 2009-12-03 | 北京汉青天朗水处理科技有限公司 | Method and apparatus for cleaning a film seperating device |
| US20110067737A1 (en) * | 2008-05-30 | 2011-03-24 | Beijing Ecojoy Water Technology Co., Ltd. | Method and apparatus for cleaning a film seperating device |
| CN102463035A (en) * | 2010-11-02 | 2012-05-23 | 赛普特环保技术(厦门)有限公司 | Coiled membrane separating technology and equipment with forward feeding and reversed washing processes |
| CN102485329A (en) * | 2011-03-22 | 2012-06-06 | 绵阳美能材料科技有限公司 | External-compression hollow fiber membrane cleaning method with no backwashing process |
| CN103232092A (en) * | 2013-05-09 | 2013-08-07 | 天津膜天膜科技股份有限公司 | Method for realizing water treatment by using pressure type continuous membrane filtering system |
| CN103232092B (en) * | 2013-05-09 | 2014-08-13 | 天津膜天膜科技股份有限公司 | Method for realizing water treatment by using pressure type continuous membrane filtering system |
| CN106823820A (en) * | 2017-03-03 | 2017-06-13 | 同济大学 | A kind of integrated apparatus for obtaining metal film operation and cleaning duty parameter |
| CN113226523A (en) * | 2018-12-27 | 2021-08-06 | 株式会社久保田 | Ultrafiltration device and method for cleaning ultrafiltration device |
| CN112717696A (en) * | 2020-12-16 | 2021-04-30 | 艾克飞膜材(嘉兴)有限公司 | Ultrafiltration membrane system cleaned by micro-bubble ozone and cleaning method thereof |
| CN114275844A (en) * | 2021-11-25 | 2022-04-05 | 上海市政工程设计研究总院（集团）有限公司 | Container immersed membrane filtering device and flushing control method thereof |
| CN114275844B (en) * | 2021-11-25 | 2024-03-08 | 上海市政工程设计研究总院（集团）有限公司 | Container immersed membrane filtering device and flushing control method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1245249C (en) | Hollow fiber membrane separator and its running process | |
| CN106794428A (en) | The cleaning method and cleaning device and water treatment system of filter membrane | |
| CN1548219A (en) | Operation method of externally pressurized hollow fiber membrane separator | |
| CN1269556C (en) | Separator system of hollow-fibre membrane in extermal pressure | |
| CN104492265A (en) | Ultrafiltration membrane device with on-line medicament backwashing and blowdown device | |
| CN108715475A (en) | A kind of water cleaning systems with pure water rinsing | |
| CN105152497B (en) | Using the circulation direct drinking advanced purification system of ozone biological activated carbon | |
| CN104192994A (en) | Membrane bioreactor | |
| CN208532494U (en) | A kind of reverse osmosis water treating equipment of ultrafiltration pretreatment | |
| CN110745910A (en) | Honeycomb ceramic membrane filtering method and filtering device | |
| CN1216674C (en) | Hollow fibre membrane separation equipment and its operation method | |
| CN107686210A (en) | The purging method of water treatment system and the water treatment system | |
| CN106955596A (en) | A kind of blue algae water separating system | |
| JP3015086U (en) | Water storage and discharge control device for reverse osmosis water machine | |
| CN1206019C (en) | Membrane separation device composed of multiple groups of membrane module and its operating method | |
| CN114195257A (en) | MBR (membrane bioreactor) water treatment equipment and water treatment method | |
| CN207845311U (en) | A kind of cutting wastewater processing system | |
| CN208617472U (en) | A kind of convection type MBR sewage treatment equipment | |
| CN217139970U (en) | Reverse osmosis membrane backwashing system | |
| CN207025102U (en) | A kind of blue algae water separating system | |
| CN2530941Y (en) | Membrane bioreactor for treatment of sewage | |
| CN206828218U (en) | A kind of water process shuts down back purge system | |
| RU22434U1 (en) | SOLUTION SEPARATION INSTALLATION | |
| CN206624739U (en) | A kind of intelligent newborn water system | |
| CN221182320U (en) | Ultrafiltration membrane assembly convenient to wash |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |