CN102417250B - Dynamic membrane purification reactor and method for removing phosphorus from regenerated water - Google Patents
Dynamic membrane purification reactor and method for removing phosphorus from regenerated water Download PDFInfo
- Publication number
- CN102417250B CN102417250B CN 201110304234 CN201110304234A CN102417250B CN 102417250 B CN102417250 B CN 102417250B CN 201110304234 CN201110304234 CN 201110304234 CN 201110304234 A CN201110304234 A CN 201110304234A CN 102417250 B CN102417250 B CN 102417250B
- Authority
- CN
- China
- Prior art keywords
- dynamic membrane
- dynamic
- membrane
- water
- suction pump
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the field of treatment of regenerated water, in particular to a dynamic membrane purification reactor and a method for removing phosphorus from regenerated water by using the same. According to a scheme adopted for realizing removal of phosphorus from regenerated water in the invention, the method comprises the following steps of: (1) setting a phosphorus removing agent dosing point and a tubular static mixer; (2) adding diatomite or kaolin and the like serving as substrates into a dynamic membrane pool; (3) attaching and coating the substrates to a dynamic membrane filtering substrate under the sucking action of a suction pump and forming a filter cake layer with intercepting and filtering functions; and (4) making water enter a water outlet pipe by passing though the filter cake layer on the surface of a dynamic membrane under the action of the suction pump and finally enter a clean water tank through a main water outlet pipe. In the invention, chemical phosphorus removal is combined with dynamic membrane filtering, chemical agents are combined with phosphorus in water into flocculating constituents in ways of adsorption, complexation, enmeshment and the like after being hydrolyzed, and the substrates, the flocculating constituents, colloid particles and the like are filtered under the filtering action of the dynamic membrane.
Description
Technical field
The present invention relates to a kind of water purification reactor and method, refer in particular to, a kind of method of utilizing the purification reactor of phosphorus in the Dynamic Membrane removal water and being applied to reused water processing.
Background technology
Carry out reuse as reuse water as the water source take municipal effluent plant effluent, urban rainwater etc. after deep purifying, this is the important channel that water resources crisis is alleviated in many cities.As landscape water, be the important way of many cities or residential quarter reclaimed water reuse with reclaimed water reuse.Landscape water is had relatively high expectations to the nutritive elements such as nitrogen, phosphorus.Studies show that phosphorus is the principal element that eutrophication " algal tufa " occurs for many lakes, municipal lake, residential quarter landscape water body etc., and the concentration of phosphorus is difficult in many municipal effluent plant effluents up to standard.
Ozone-biological active carbon (O
3-BAC), the technology such as membrane bioreactor (MBR) uses comparatively extensive in reused water processing.But, O
3-MBR investment and running cost are higher, be subject to the film pollution and cause membrane flux to descend, and the MBR phosphor-removing effect is limited.O
3-BAC is applied to larger regeneration water factory usually, but uses less to middle and small scale or distributed regeneration water station; Equally, O
3-BAC phosphor-removing effect is also very limited.
Dynamic Membrane refers to that its filtering substrate is microgrid material (bolting silk, non-woven fabrics, nylon screen etc.) by the new film with solid-liquid separation capability of mixed solution in precoating paint or the reaction tank in base net or the formation of macropore supporter (such as stainless (steel) wire) surface.The advantage of Dynamic Membrane is fine to the particulate matter removal effect, and delivery turbidity can be controlled at below the 0.1NTU.In addition, Dynamic Membrane is particularly useful for the distributing reuse water cleaning project of middle and small scale.But Dynamic Membrane belongs to apply in essence filters (Precoat filtration), mainly removes the particulate form pollutent by mechanical grading and crown_interception, does not almost have the dephosphorization ability.How to improve the phosphor-removing effect of dynamic membrane filtering process, this is to expand the important way that the dynamic membrane filtering technology is used in reused water processing.
The present invention is directed to the problems referred to above, take Dynamic membrane as the basis, improve the adsorption and dephosphorization work in order to improve the dynamic membrane filtering process to the removal effect of phosphorus in the reuse water by strengthening.The present invention can be applicable to the municipal wastewater treatment plant deep purifying, also can be applicable to the reused water processing engineering take municipal effluent plant effluent or rainwater as the water source.
Summary of the invention
One of purpose of the present invention is: a kind of Dynamic Membrane purification reactor with good dephosphorization ability is provided;
Another object of the present invention is: a kind of method of utilizing the Dynamic Membrane purification reactor to carry out reused water processing is provided.
In order to realize removing the purpose of phosphorus in the reuse water, the present invention takes following technical scheme:
Dynamic Membrane purification reactor of the present invention comprises that water inlet pipe, dephosphorization agent add point, static mixer, water-in, current stabilization district, matrix and add point, dynamically membrane cisterna, dynamic film component, aeration tube, mud collection area, shore pipe, blast main valve, air compressor, tensimeter, suction pump, rising pipe valve, back flushing, backwash tube valve etc.
Be provided with dephosphorization agent at dynamic membrane cisterna water inlet pipe and add a little and static mixer, fully mix with pending water through static mixer after dephosphorization agent adds.
One perforation plate is installed in the described dynamic membrane cisterna, and the top in the space that forms between a side of described perforation plate and the pool wall of this dynamic membrane cisterna is set to opening, is provided with matrix at this opening and adds a little; Opposite side at described perforation plate is equipped with described dynamic film component formation dynamic membrane filtering district; Described aerating apparatus is installed below dynamic film component, and this aerating apparatus is connected with described air compressor by described aerating pipelines, and the below of described aerating apparatus is provided with described sludge sump.
Be provided with pressure lock on the described aerating pipelines.In the described sludge sump shore pipe is installed.
Described rising pipe is installed above described dynamic film component, and described rising pipe is connected with described suction pump.On described rising pipe and the rising pipe that suction pump is connected tensimeter and rising pipe valve are installed.
Definite method of the usage quantity of described dynamic film component be so that the membrane flux of Dynamic Membrane at 30～300L/m
2Between the h.
Described dynamic film component form is flat sheet membrane, and material is that the aperture is the bolting silk of 0.1～0.2mm.The pore diameter range of Dynamic Membrane is between 0.01～0.20 μ m, and the membrane flux of Dynamic Membrane is 30～300L/m
2H.The hydraulic detention time of water in the membrane filtration district that dynamic film component is installed is 10～40 minutes.
One exit branch is set above each described dynamic film component, and all exit branch are finally incorporated the outfall sewer of a Dynamic Membrane into; Being provided with suction pump in the outfall sewer of Dynamic Membrane takes the Dynamic Membrane water outlet away.
Matrix adds by described matrix and a little adds after the described dynamic membrane cisterna, under the suction function that the suction of the suction pump that the outfall sewer of Dynamic Membrane arranges forms, matrix is adhered to be coated on the dynamic membrane filtering base material and to form and is had the cake layer of holding back filtering function.
Described matrix is diatomite, kaolin or its mixture by any ratio; Described matrix can add continuously or intermittently add.
Described matrix add method for determination of amount be so that in the membrane cisterna suspended material concentration between 1g/L～200g/L.
Described dephosphorization agent is one or more the mixture in molysite, aluminium salt, hydronium(ion) oxidation iron, hydrous iron oxide, W 4600, the aluminum oxyhydroxide.
Described molysite is one or more the mixing salt in iron trichloride, ferric sulfate, poly-ferric chloride, the bodied ferric sulfate; Described aluminium salt is one or more the mixing salt in aluminum chloride, Tai-Ace S 150, polymerize aluminum chloride, the polyaluminium sulfate.
Described dephosphorization agent to add method for determination of amount be the quality sum that makes iron and aluminium in the dephosphorization agent with water in the ratio of mass concentration of phosphorus be 1: 1～20: 1.
Dynamically the current in the membrane cisterna are that suction function by suction pump is accomplished through dynamic film component.Under the suction function that the suction of the suction pump that the outfall sewer of Dynamic Membrane arranges forms, dynamically the water in the membrane cisterna enters the inboard from the film outside, and is finally flowed out by outfall sewer via the exit branch of dynamic film component.The suction negative pressure control that suction pump forms on the surface of dynamic film component is between 10kPa～60kPa.
Add dephosphorization agent in the pending water and enter dynamic membrane cisterna after fully mixing by static mixer and water, be coated in the cake layer of holding back filtering function that has that forms on the Dynamic Membrane base material by being adhered to by matrix afterwards, the particulate form phosphorus that is adsorbed on the hydrolysate surface of dephosphorization agent or dephosphorization agent is removed from water holding back under the filteration of cake layer.
The present invention further arranges a Dynamic Membrane backwashing water house steward, and each dynamic film component arranges a backwashing water arm; In Dynamic Membrane backwashing water house steward, be provided with the Dynamic Membrane backwashing pump.The rising pipe that namely is connected with described suction pump at described rising pipe is connected with a Dynamic Membrane backwashing water house steward, this Dynamic Membrane backwashing water house steward is connected with the Dynamic Membrane backwashing pump, and rising pipe is positioned on the rising pipe of described suction pump top with the Dynamic Membrane backwashing water house steward place of being connected.On described Dynamic Membrane backwashing water house steward's the pipeline backwash tube valve is installed.
In order to guarantee membrane flux, in the dynamic film component operational process, need regularly dynamic film component to be carried out back flushing.When dynamic film component carried out back flushing, the water outlet after the film backwashing pump filters dynamic film component pumped into the inboard and laterally outflow of dynamic film component, and the pollutent that is attached to the film surface is able to break away from from the film surface.The cycle of dynamic film component back flushing is 0.5～20 minute.
When the film backwashing pump is opened, back flushing water inlet pipe valve opening, and suction pump is out of service and the rising pipe valve closes; After back flushing stops, back flushing water inlet pipe valve closes, and suction pump brings into operation and the rising pipe valve opening.
Described air compressor pumps into pressurized air in the water in dynamic membrane filtering district, thereby for dissolved oxygen is provided in the water, and provide hydraulic action to carry out mix and blend and shear the dirt settling of cleaning the Dynamic Membrane surface.Pressurized air can be to pass into constantly, also can be to pass into off and on.The gas-water ratio scope in membrane filtration district is 5: 1～100: 1 (m
3: m
3).Described aerating apparatus can be that boring aeration pipe, aeration are first-class.
In the present invention, the particulate matter that density is larger in the water, flco, dephosphorization agent or its hydrolysate etc. enter sludge sump under action of gravity, and by shore pipe the mud in the sludge sump are discharged.Sludge discharging period can be 12～72 hours.
Of the present inventionly utilize above-mentioned Dynamic Membrane purification reactor to carry out the method for reused water processing:
Add dephosphorization agent in pending water, dephosphorization agent fully mixes with pending water by static mixer and contacts.If the dephosphorization agent that adds is molysite or aluminium salt, then hydrolysis formation iron salt hydrolysis product or aluminium salt hydrolysis product occur in molysite or aluminium salt; Dephosphorization agent or its hydrolysate are converted into particulate form phosphorus by effects such as electrostatic adhesion, surface hydroxyl complexings with dissolved phosphorus in the water.
The water that has added dephosphorization agent enters the current stabilization district of dynamic membrane cisterna from the opening of dynamic membrane cisterna, enters afterwards the membrane filtration district of dynamic membrane cisterna through porous plate.Add a little from the matrix of dynamic membrane cisterna and to dynamic membrane cisterna, to add matrix; Matrix in the membrane filtration district forms cake layer at the Dynamic Membrane substrate surface under the effect of the negative pressure that suction pump forms.
Water in the dynamic membrane cisterna passes the Dynamic Membrane surface under the effect of suction pump cake layer enters rising pipe, and finally enters in the clean water basin by outfall sewer.In carrying out dynamic membrane cisterna operational process, air compressor can continue or pump into off and on pressurized air so that dissolved oxygen to be provided, and provides hydraulic action to carry out mix and blend and shear the dirt settling of cleaning the Dynamic Membrane surface.Water in the membrane filtration district passes the film surface of dynamic film component under the effect of suction pump cake layer enters in the intermediate pool.
Described matrix add method for determination of amount be so that in the membrane cisterna suspended material concentration between 1g/L～200g/L.
Described matrix is diatomite, kaolin or its mixture by any ratio.
Described dephosphorization agent is one or more the mixture in molysite, aluminium salt, hydronium(ion) oxidation iron, hydrous iron oxide, W 4600, the aluminum oxyhydroxide.
Described dephosphorization agent to add method for determination of amount be the quality sum that makes iron and aluminium in the dephosphorization agent with water in the ratio of mass concentration of phosphorus be 1: 1～20: 1.
In the dynamic film component operational process, need regularly dynamic film component to be carried out back flushing.When dynamic film component carried out back flushing, the water outlet after the film backwashing pump filters dynamic film component pumped into the inboard and laterally outflow of dynamic film component, and the pollutent that is attached to the film surface is able to break away from from the film surface.The cycle of dynamic film component back flushing is 0.5～20 minute.
Description of drawings
Fig. 1 is the Dynamic Membrane purification reactor.
Reference numeral
1, intake pump 2, tubular static mixer 3, dephosphorization agent add mouth
4, current stabilization district 5, matrix add a little 6, membrane cisterna
7, dynamic film component 8, aeration tube 9, mud collection area
10, shore pipe 11, blast main valve 12, air compressor
13, tensimeter 14, suction pump 15, rising pipe valve
16, backwashing pump 17, backwash water tube valve
The present invention has following advantage:
1, can only remove colloidal solid phase ratio with respect to general Dynamic Membrane reactor, the present invention can significantly improve the removal effect of phosphorus on this basis, can be applicable to the reuse water deep purifying;
2, the present invention can design neatly according to treatment scale, is particularly suitable for middle-size and small-size reuse water cleaning project and urban rainwater reuse project;
3, the operations such as dynamic membrane filtering, back flushing, aeration can be realized automatic control easily, and operational management is convenient.
Embodiment
Embodiment 1
See also figure, Dynamic Membrane purification reactor of the present invention comprises chemical dephosphorization device 2 and dynamic membrane cisterna 6 two portions, and the chemical dephosphorization device is positioned at before the dynamic membrane cisterna.Wherein, the chemical dephosphorization device comprises that tubular static mixer 2, dephosphorization agent add mouth 3 etc.; The Dynamic Membrane purification reactor comprises that current stabilization district 4, matrix add a little 5, membrane filtration district 6, dynamic film component 7, aeration tube 8, mud collection area 9, shore pipe 10, blast main valve 11, air compressor 12, tensimeter 13, suction pump 14, rising pipe valve 15, backwashing pump 16, backwash tube valve 17 etc.;
One perforation plate is installed between described current stabilization district 4 and the membrane filtration district 6, and the top in the space that forms between a side of described perforation plate and the pool wall in membrane filtration district 6 is set to opening, is provided with matrix at this opening and adds a little 5; Opposite side at described perforation plate is equipped with described dynamic film component 7 formation dynamic membrane filtering districts; Described aerating apparatus 8 is installed below dynamic film component, and this aerating apparatus 8 is connected with described air compressor 12 by described aerating pipelines 8, and the below of described aerating apparatus 8 is provided with described sludge sump 9.Be provided with pressure lock 11 on the described aerating pipelines; Shore pipe 10 is installed in the described sludge sump.Described rising pipe is installed above described dynamic film component 7, and described rising pipe is connected with described suction pump 14.On described rising pipe and the rising pipe that suction pump 14 is connected tensimeter 13 and rising pipe valve 15 are installed.
In described membrane filtration district 4 groups of described dynamic film components 7 are installed and form the membrane filtration district, described dynamic film component is flat sheet membrane, and its material is the bolting silk material; The aperture of Dynamic Membrane is 0.1mm, and the membrane flux of Dynamic Membrane is 60L/m
2H.
One exit branch is set above each described dynamic film component, and all exit branch are finally incorporated the outfall sewer of a Dynamic Membrane into; Being provided with suction pump 14 in the outfall sewer of Dynamic Membrane takes the Dynamic Membrane water outlet away.A Dynamic Membrane backwashing water house steward is set, and each dynamic film component arranges a backwashing water arm; In Dynamic Membrane backwashing water house steward, be provided with Dynamic Membrane backwashing pump 16.The rising pipe that namely is connected with described suction pump at described rising pipe is connected with a Dynamic Membrane backwashing water house steward, this Dynamic Membrane backwashing water house steward is connected with the Dynamic Membrane backwashing pump, and rising pipe is positioned on the rising pipe of described suction pump top with the Dynamic Membrane backwashing water house steward place of being connected.On described Dynamic Membrane backwashing water house steward's the pipeline backwash tube valve 17 is installed.
Described chemical dephosphorization device is a tubular static mixer 2, leaves dephosphorization adding of agent mouth 3 on the mixing tank.
Utilize above-mentioned Dynamic Membrane purification reactor to carry out the method for reuse water dephosphorization:
Pending water enters tubular static mixer 2 after water pump 1 pressurization, add continuously the dephosphorization medicament by adding of agent mouth 3, after the medicament hydrolysis, the phosphorus of sweeping etc. in mode and the water by absorption, complexing, volume is combined into flco, then flow into the current stabilization district of dynamic membrane cisterna, enter afterwards the membrane filtration district of dynamic membrane cisterna through porous plate.
Add a little from the matrix of dynamic membrane cisterna and to dynamic membrane cisterna, to add matrix; Matrix in the membrane filtration district forms cake layer at the Dynamic Membrane substrate surface under the effect of the negative pressure that suction pump forms; Matrix, flco, colloidal solid thing etc. are removed the holding back under the filteration of cake layer that the Dynamic Membrane substrate surface forms.
Water in the dynamic membrane cisterna passes the Dynamic Membrane surface under the effect of suction pump cake layer enters rising pipe, and finally enters in the clean water basin by outfall sewer.The hydraulic detention time of water in the membrane filtration district that dynamic film component is installed is 10～40 minutes.
With the water in suction pump suction membrane filtration district, the suction negative pressure control that suction pump forms on the surface of dynamic film component is between 10kPa～60kPa.Water in the dynamic membrane filtering district passes dynamic film component under the effect of suction pump film surface enters rising pipe, and finally enters in the clean water basin by outfall sewer.The particulate form pollutents such as water-borne glue body, flco then are trapped at this moment, and the particle that most of density is larger enters under the gravity settling effect in the sludge sump 9, and finally get rid of from dynamic membrane cisterna 6 by shore pipe 10; Need to carry out backwash operation behind the dynamic film component 7 operation certain hours, at this moment, open film backwashing pump 16, and the water outlet after the dynamic film component filtration is pumped into the inboard of dynamic film component and laterally outflow, the pollutent that is attached to the film surface of dynamic film component is able to from the disengaging of film surface; Air compressor 12 can continue or pump into off and on pressurized air so that dissolved oxygen to be provided, and provides hydraulic action to carry out mix and blend and shear the dirt settling of cleaning the Dynamic Membrane surface, and the gas-water ratio scope in membrane filtration district is 5: 1～100: 1 (m
3: m
3).
Chemical oxygen demand COD in the pending water
CrConcentration is 30mg/L, and ammonia nitrogen concentration is 4mg/L.Adopt aforesaid method to process the water outlet chemical oxygen demand COD
CrConcentration is 10mg/L, and ammonia nitrogen concentration is 0.5mg/L.
Claims (8)
1. Dynamic Membrane purification reactor, it comprises chemical dephosphorization and dynamic membrane cisterna two portions, and chemical dephosphorization is positioned at before the dynamic membrane cisterna; Wherein, chemical dephosphorization comprises that tubular static mixer, dephosphorization agent add mouth; Dynamically membrane cisterna comprises that current stabilization district, matrix add point, membrane cisterna, dynamic film component, aeration tube, mud collection area, shore pipe, blast main valve, air compressor, tensimeter, suction pump, rising pipe valve, backwashing pump, backwash tube valve; It is characterized in that:
One perforation plate is installed in the described dynamic membrane cisterna, and the top in the space that forms between a side of described perforation plate and the pool wall of this dynamic membrane cisterna is set to opening, is provided with matrix at this opening and adds a little; Opposite side at described perforation plate is equipped with described dynamic film component formation dynamic membrane filtering district; Aerating apparatus is installed below dynamic film component, and this aerating apparatus is connected with described air compressor by described aeration tube, and the below of described aerating apparatus is provided with sludge sump;
Be provided with pressure lock on the described aeration tube; In the described sludge sump shore pipe is installed;
Rising pipe is installed above described dynamic film component, and described rising pipe is connected with described suction pump; On described rising pipe and the rising pipe that suction pump is connected tensimeter and rising pipe valve are installed.
2. Dynamic Membrane purification reactor according to claim 1, it is characterized in that dynamic film component usage quantity definite method for so that the membrane flux of Dynamic Membrane at 30～300L/m
2Between the h.
3. Dynamic Membrane purification reactor according to claim 1 and 2, it is characterized in that described dynamic film component form is flat sheet membrane, filtering substrate is the microgrid material, and the pore diameter range of Dynamic Membrane is between 0.01～0.20 μ m, and the membrane flux of Dynamic Membrane is 30～300L/m
2H; One exit branch is set above each described dynamic film component, and all exit branch are finally incorporated the outfall sewer of a Dynamic Membrane into; Being provided with suction pump in the outfall sewer of Dynamic Membrane takes the Dynamic Membrane water outlet away.
4. Dynamic Membrane purification reactor according to claim 3 is characterized in that matrix adds by described matrix a little to add into described dynamic membrane cisterna; And matrix is under the suction function that the suction of the suction pump that the outfall sewer of Dynamic Membrane arranges forms, and adheres to be coated on the dynamic membrane filtering base material and to form to have the cake layer of holding back filtering function.
5. Dynamic Membrane purification reactor according to claim 4 is characterized in that the matrix that adds is diatomite or kaolin.
6. the described Dynamic Membrane purification reactor of any one carries out the method for reused water processing according to claim 1～5, it is characterized in that: add the dephosphorization chemical agent in the pending water, the process tubular static mixer is finished mixing process, adds in matrix afterwards a little to add matrix and enter the dynamic membrane filtering district behind the current stabilization district;
Matrix in the dynamic membrane filtering district forms cake layer at the Dynamic Membrane substrate surface under the suction function that suction pump forms; Water in the dynamic membrane filtering district then passes the film surface of Dynamic Membrane under the effect of the negative pressure that suction pump forms cake layer enters rising pipe, and finally enters in the clean water basin by outfall sewer;
In the Dynamic Membrane backwash process, air compressor intermittently pumps into pressurized air;
The space that forms between one side of described perforation plate and the pool wall of described dynamic membrane cisterna has consisted of described current stabilization district.
7. method according to claim 6, it is characterized in that: the hydraulic detention time in described dynamic membrane filtering district is 10～40 minutes;
The suction negative pressure control that described suction pump forms on the surface of dynamic film component is between 10kPa～60kPa.
8. method according to claim 6, it is characterized in that: the gas-water ratio scope during the Dynamic Membrane back flushing is 5: 1～100: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110304234 CN102417250B (en) | 2011-10-10 | 2011-10-10 | Dynamic membrane purification reactor and method for removing phosphorus from regenerated water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110304234 CN102417250B (en) | 2011-10-10 | 2011-10-10 | Dynamic membrane purification reactor and method for removing phosphorus from regenerated water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102417250A CN102417250A (en) | 2012-04-18 |
| CN102417250B true CN102417250B (en) | 2013-03-20 |
Family
ID=45941928
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110304234 Expired - Fee Related CN102417250B (en) | 2011-10-10 | 2011-10-10 | Dynamic membrane purification reactor and method for removing phosphorus from regenerated water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102417250B (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103755071B (en) * | 2014-01-10 | 2015-12-30 | 安徽锋亚环境技术有限公司 | For the emergent dephosphorization adsorption unit of micro-eutrophication city landscape water body |
| CN104276730A (en) * | 2014-10-20 | 2015-01-14 | 上海稳上创新技术有限公司 | Efficient intensive nitrogen and phosphorus removal sewage treatment process |
| CN104876364A (en) * | 2015-05-27 | 2015-09-02 | 江苏省嘉庆水务发展有限公司 | Complete set of device for efficient advanced treatment of wastewater |
| CN108033653A (en) * | 2018-01-08 | 2018-05-15 | 浙江利欧环境科技有限公司 | A kind of addition method of city domestic sewage dephosphorization agent and alkali |
| CN110575687B (en) * | 2019-04-24 | 2021-08-13 | 上海蓝宇水处理股份有限公司 | Negative pressure water treatment device and filtering method and back flushing method thereof |
| CN110255806A (en) * | 2019-07-05 | 2019-09-20 | 南京中微纳米功能材料研究院有限公司 | A kind of sewage device of ferrite dynamic film process heavy metal |
| CN111039658A (en) * | 2019-12-31 | 2020-04-21 | 广东省水利水电科学研究院 | Phosphorus removal ceramsite and preparation method thereof |
| CN113548741A (en) * | 2020-04-23 | 2021-10-26 | 南京信息工程大学 | High-turbidity water treatment method and treatment device thereof |
| CN112661234A (en) * | 2021-01-22 | 2021-04-16 | 山东颖慧园环保科技有限公司 | Efficient phosphorus removal agent for sewage treatment and preparation method thereof |
| CN113044922A (en) * | 2021-03-15 | 2021-06-29 | 北控水务(中国)投资有限公司 | Sewage treatment method |
| CN113697903A (en) * | 2021-07-21 | 2021-11-26 | 利得膜(北京)新材料技术有限公司 | Zero-medicament short-flow membrane direct filtration system and sewage treatment method |
| CN113461293A (en) * | 2021-07-23 | 2021-10-01 | 南京信息工程大学 | Low-concentration sludge dewatering method and device based on dynamic membrane separation |
| CN116854238A (en) * | 2023-08-14 | 2023-10-10 | 江苏吉尧新材料科技有限公司 | Blue algae filter equipment of biomembrane |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1821112A (en) * | 2006-03-06 | 2006-08-23 | 山东大学 | Intensified mixed coagulation and dynamic film integrated waste water treating process |
| CN1843971A (en) * | 2006-04-19 | 2006-10-11 | 山东大学 | Back-flushing operation method of dynamic membrane bioreactor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003062591A (en) * | 2001-08-27 | 2003-03-04 | Ebara Corp | Method for purifying organic waste water |
-
2011
- 2011-10-10 CN CN 201110304234 patent/CN102417250B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1821112A (en) * | 2006-03-06 | 2006-08-23 | 山东大学 | Intensified mixed coagulation and dynamic film integrated waste water treating process |
| CN1843971A (en) * | 2006-04-19 | 2006-10-11 | 山东大学 | Back-flushing operation method of dynamic membrane bioreactor |
Non-Patent Citations (3)
| Title |
|---|
| A/O-化学除磷工艺中DMBR动态膜成膜条件研究;梁思懿等;《辽宁城乡环境科技》;20070228;第27卷(第01期);24-26、36 * |
| JP特开2003-62591A 2003.03.04 |
| 梁思懿等.A/O-化学除磷工艺中DMBR动态膜成膜条件研究.《辽宁城乡环境科技》.2007,第27卷(第01期),24-26、36. |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102417250A (en) | 2012-04-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102417250B (en) | Dynamic membrane purification reactor and method for removing phosphorus from regenerated water | |
| CN102417273B (en) | Dynamic membrane purifying reactor and method for removing ammonia nitrogen and organic matters from reclaimed water | |
| CN102336493B (en) | Reaction device for deep treatment of drinking water and method for deep treatment of drinking water by water factory | |
| CN202516410U (en) | Precipitation and filtering compounding tank | |
| CN101224357A (en) | Two-stage dynamic membrane filtering method for printing and dyeing wastewater recycling | |
| CN101565247A (en) | Zero-discharge purifying treatment method for mine wastewater and mine domestic sewage | |
| CN109160641A (en) | A kind of processing unit synchronizing suspended matter, organic matter and nitrogen phosphorus in water removal | |
| CN103466876A (en) | External double-stage membrane bioreactor | |
| CN103073122A (en) | Vehicular emergency drinking water purifying station | |
| CN203999258U (en) | The integrated Sewage treatment systems in a kind of cement mill | |
| CN102060393A (en) | Treatment method and equipment of sporadic pollutant source water | |
| CN106007169A (en) | Method for effectively retarding ultrafiltration membrane pollution by using in-situ Fe(OH)3 floccules and nano-iron | |
| CN106673257A (en) | Micropolluted raw water treatment integrated plant | |
| CN206395957U (en) | A kind of cleaning system of drinking water system | |
| CN209259830U (en) | Synchronize the processing unit of suspended matter, organic matter and nitrogen phosphorus in water removal | |
| CN209161671U (en) | Integrative water purifying device | |
| CN105582813B (en) | A kind of high-throughput Dynamic membrane-separation device of dirt water pollutant concentration | |
| CN215517060U (en) | Landfill leachate pretreatment system | |
| CN201882983U (en) | Equipment used for treating water of slight-polluted and gustily-polluted water source | |
| CN110342686A (en) | Utilize chemical precipitation-absorption method removal ammonia nitrogen in sewage sewage disposal system | |
| CN212610143U (en) | Energy-saving landfill leachate treatment facility | |
| CN108383238A (en) | A kind of bio-matrix biofilm pipeline infiltration sewage disposal system | |
| CN208603895U (en) | River water cleaning processing system | |
| CN113830934B (en) | Purification treatment system and process for surface water or urban landscape water | |
| CN218357909U (en) | Ecological concrete composite water purification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130320 Termination date: 20141010 |
|
| EXPY | Termination of patent right or utility model |