CN103121760A - Reverse-osmosis seawater desalination pretreatment method and device for polluted sea areas - Google Patents
Reverse-osmosis seawater desalination pretreatment method and device for polluted sea areas Download PDFInfo
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- CN103121760A CN103121760A CN2011103668410A CN201110366841A CN103121760A CN 103121760 A CN103121760 A CN 103121760A CN 2011103668410 A CN2011103668410 A CN 2011103668410A CN 201110366841 A CN201110366841 A CN 201110366841A CN 103121760 A CN103121760 A CN 103121760A
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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
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Abstract
The invention relates to reverse-osmosis seawater desalination pretreatment method and device for polluted sea areas. The technical scheme of the reverse-osmosis seawater desalination pretreatment device includes that a silt precipitation tank with conical section is arranged on the lower portion of a common micro- and ultra-filtration membrane tank body, a solid and liquid separation area is arranged in the middle of the common micro- and ultra-filtration membrane tank, and water is fed from the solid and liquid separation area. By the aid of the structure of the reverse-osmosis desalination pretreatment device, recovery rate of the system can be effectively increased, disturbance on membrane component from water impact is avoided, stability of outlet water quality is guaranteed, energy is saved and consumption is reduced.
Description
Technical field
The invention belongs to water-treatment technology field, be specifically related to a kind of reverse osmosis seawater desalting pretreatment process and device that pollutes the marine site.
Background technology
The mankind face serious fresh water problem in short supply in 21 century, water resources lacks has become the significant problem that is related to poverty, Sustainable development and even international peace and security, therefore sea water desaltination more and more comes into one's own, utilize desalination technology to produce cleaning water from seawater, become a kind of important means that people obtain fresh water.
The main method for desalting seawater that adopts in the world at present comprises in multistage flash evaporation (MSF), multiple-effect evaporation (MED), reverse osmosis (RO), the RO technology obtains using comparatively widely because it has the advantages such as less investment, easy to operate, the construction period is short, floor space is little, and the ratio of occupying in sea water desaltination has year by year the trend that increases, and in the sea water desaltination market of 21 century, sea-water reverse osmose (SWRO) will be main method for desalting seawater.Yet guaranteeing that reverse osmosis unit can move steadily in the long term, is vital to water pretreatment.
At present, the conventional pretreatment process of sea water desaltination mainly comprises flocculation, precipitation, multi-medium filtering, barrel type filtering, charcoal absorption filtration etc.Flocculation, precipitation, media filtration can be removed most of colloid and suspended solids.Core strainer can prevent that the particle in feed water, pharmaceutical chemicals feeding unit or pre-treatment medium from entering the RO system, with protection RO film, therefore claim again cartridge filter.The normal polypropylene fibre filter core that adopts, aperture size mostly is 1-10 μ m, and some outfit double medium filtrations are to provide the more filtration of deep layer.When the source quality of seawater was normal and stable, this pretreatment process can be down to 2-3 with the SDI value of RO system water inlet.But when the seawater source quality fluctuateed or is subject to polluting, its effluent quality also fluctuateed, and can not guarantee that effluent quality satisfies the pre-treatment requirement; Gac also for bacterium provides nutrition source, causes secondary pollution when having adsorbed organism.Conventional pretreatment process can not consist of effective barrier to bacterium and colloidal solid, and protection RO film extends its work-ing life, and produces discharge and water quality all changes with raw water quality, can not satisfy the constant requirement of RO influent quality.Compare with conventional treatment method, little, ultrafiltrationmembrane process has several large advantages: 1. floor space is little, and level of automation is high; 2. investment and working cost reduce; 3. the water quality after processing obviously is better than conventional processing method effluent quality, the work-ing life of effectively controlling diaphragm pollution when entering reverse osmosis membrane system, prolongation film.
Sea water desaltination is little, the pretreated core of ultrafiltrationmembrane process be little, can ultrafiltration membrane system be stablized, the operation of efficient low-consume ground.During at present film system operation, the mode that top water inlet usually, bottom draining, membrane module adopt suction pump to aspirate water outlet is moved.The water impact meeting disturbance membrane module of top water inlet, when serious, fracture of wire occurs in hollow fiber film thread under water impact, causes effluent quality to worsen.When membrane module operation pressure reduction increases, carry out general waterpower when cleaning, to clean and advance again water and filter all rinse water in membrane cisterna are emptying after finishing, this operation needs a large amount of ultrafiltration to produce water, causes the rate of recovery of system to reduce.
Summary of the invention
The objective of the invention is the problem that exists for the membrane cisterna structure in existing film system, a kind of optimization membrane cisterna flow condition and influent quality are provided, energy-saving and cost-reducing, improve Novel immersed membrane pond little, the ultrafiltration system rate of recovery.And on this basis, for the problem of polluting in marine site sea water desaltination preprocessing technical field, provide a kind of sea water desaltination pretreatment process that can guarantee seawater desalination reverse osmosis film system stable operation, effectively controlling diaphragm pollution, extend membrane lifetime.
Purpose of the present invention can reach by following scheme and measure:
A kind of immersed type membrane pond with the taper slot part, described membrane cisterna comprise pond body (1), water-in and pipeline (2), water port and pipeline (3), water outlet and pipeline (4) and membrane module (5); The bottom of pond body (1) is the heavy mud groove of cross section taper, and the middle part is solid-liquid displacement zone, and top is for putting the film district; Membrane module is placed in the film district, and water-in is positioned at solid-liquid displacement zone; Water port is positioned at the lowest part of heavy mud groove; Water outlet is positioned at the top of putting the film district.
In the cross-sectional height of above-mentioned pond body, heavy mud groove and solid-liquid displacement zone and the aspect ratio of putting the film district are preferably: (4～8): 1: (1.1～1.4).
The present invention also provides a kind of sea water desaltination pretreatment process that pollutes the marine site, uses above-mentioned immersed type membrane pond with the taper slot part in the method.
The method includes the steps of:
Pending water enters immersed type membrane pond with the taper slot part by service pump, after this pending water enters solid-liquid displacement zone, the flco of larger particles material and suspension sinks in the mud groove, after the water in upper deployment film district directly filters by membrane module, adopts the suction of siphon or pump to discharge from water outlet.
Above-mentioned pending water first passes through preoxidation operation and/or coagulation operation before entering immersed type membrane pond with the taper slot part by service pump.
In described preoxidation operation, the preoxidation agent of use is one or more in ozone, potassium permanganate or potassium ferrate.Ozone dosage is 0.5-10mg/L, and the potassium permanganate dosage is 0.5-10mg/L, and the potassium ferrate dosage is 0.5-10mg/L.
In described coagulation operation, the coagulating agent of use is one or more in iron trichloride or polymerize aluminum chloride.The dosage of iron trichloride is 1-8mg/L (in iron), and the dosage of polymerize aluminum chloride is 1-10mg/L (in aluminium).
In the sea water desaltination pretreatment process in above-mentioned pollution marine site, also contain the film system and regularly generally clean or the matting step; Described general cleaning step is: adopt ultrafiltration to produce the combined cleaning of the direct backwash of water and air purge, and standing 10-30 minute, open the scupper valve goalkeeper solid-liquid displacement zone of membrane cisterna bottom and the rinse water in heavy mud groove district and discharged by water port, carry out ultra-filtration filters; Matting is first generally to clean, and then membrane module is carried out the combined cleaning of medicament backwash and air purge, and cleaning is carried out ultra-filtration filters after finishing.
Described chemical agent is that clorox, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, sodium hydroxide or other films clean one or more in medicament commonly used; Dosing method is for adding separately or adding simultaneously.
Above-mentioned a kind of immersed type membrane pond with the taper slot part, putting the submerged membrane of placing in the film district is hollow-fibre membrane, flat sheet membrane or tubular membrane; Membrane material is polyvinylidene difluoride (PVDF), polysulfones, polyvinyl chloride or polyethersulfone; Membrane pore size is at 0.01-1 μ m.
In sum, principal feature of the present invention is:
The heavy mud groove of cross section taper is set by the bottom at the Chi Tishang of common little, ultrafiltration membrane cisterna, and the middle part arranges solid-liquid displacement zone, and adopts middle part solid-liquid displacement zone water inlet.The contrast of the structure of this pond body and common membrane cisterna pond body have the following advantages:
(1) but the heavy mud groove of the cross section taper of membrane cisterna bottom can be collected the flco, mud of particulate matter contained in water inlet and sedimentation etc. effectively, when general cleaning the (non-chemically cleaning) end or membrane cisterna blowdown, only need the part water yield of discharging membrane cisterna bottom, the blowdown effect can be played and need not water all in the emptying membrane cisterna, the rate of recovery of system can be effectively improved like this;
(2) on the solid-liquid displacement zone at membrane cisterna middle part, water-in is set, after water enters membrane cisterna, in solid-liquid displacement zone, but particulate matter and sedimentation flco etc. sink to the heavy mud groove of bottom, filter in the film district of putting that supernatant liquor enters top, and controlling diaphragm pollutes so effectively, puies forward high yield water water quality; Water enters from the solid-liquid displacement zone at middle part, also can avoid water impact to the disturbance of membrane module, thereby prevents that effectively hollow fiber film thread from the problem of fracture of wire occuring under water impact, guarantees the stability of effluent quality;
(3) in membrane cisterna, the bottom arranges respectively the placing height that solid-liquid displacement zone and heavy mud groove can improve membrane module, is convenient to utilize liquid level difference to carry out the siphon water outlet, and is energy-saving and cost-reducing; Open suction pump suction water outlet can't the siphon water outlet after causing transmembrane pressure to increase the time when polluting due to film.
Polluting treatment process contrast and the conventional treatment method that adopts preoxidation-In-line coagulation-micro-filtration or ultrafiltration in the marine site, have following advantage: (1) floor space is little, and level of automation is high; (2) investment and working cost reduce; (3) water quality after the processing obviously is better than conventional processing method effluent quality, and preoxidation effectively changes the character of natural organic matter in seawater, the work-ing life of effectively controlling diaphragm pollution when entering reverse osmosis membrane system, prolongation film.
Description of drawings
Fig. 1 is the simplified schematic diagram with the immersed type membrane pond of taper slot part.
In figure, (1) pond body; (2) water-in and pipeline; (3) water port and pipeline; (4) water outlet and pipeline; (5) membrane module; (6) water tank is produced in ultrafiltration; (7) suction pump; (8) backwashing pump.
Fig. 2 is sea water desaltination pretreatment process FB(flow block).
Embodiment
Permanganate index (COD in embodiment
Mn) mensuration according to the difference of former water chloride ion content, adopt permanganate index acid process or basic process (State Standard of the People's Republic of China GB119114-89); The mensuration of turbidity adopts the turbidimeter (model: HACH2100AN) of U.S. Hash company; The mensuration of specific conductivity adopts the portable electric electrical conductivity instrument (model: HACH Sension 5) of U.S. Hash company; The mensuration of pH adopts the portable pH meter (model: HACH Sension2) of U.S. Hash company.
According to a kind of reverse osmosis seawater desalting pretreatment process and device that pollutes the marine site of the present invention, comprise pre-sink device, raw water pump, preoxidation device, intake pump, coagulant dosage device, suction pump, backwashing pump, little/ultrafiltration immersed type membrane pond, ultrafiltration product water tank.Preoxidation device outlet conduit is connected with intake pump, and the coagulant dosage device is set before above-mentioned intake pump, intake pump is connected through the water-in of the solid-liquid displacement zone at control valve and immersed type membrane pond middle part, immersion type membrane component is placed in the submergence pond, the water outlet pipe valve is connected to the product water tank by pipeline or suction pump, and the backwash pipeline is by producing water tank through backwashing pump junctional membrane assembly.
Embodiment 1
Certain marine site seawater a is adopted in this test, and the water quality situation is as shown in table 1.
Table 1 raw water quality table
| Index | Turbidity (NTU) | COD Mn(mg/L) | pH |
| Raw water quality | 150-300 | 4.8 | 7.8-8.8 |
By as seen from Table 1, raw water quality belongs to III class water body, and water body is polluted, and wherein particulate matter is more.System's operation process is preliminary sedimentation-potassium ferrate oxidation-In-line coagulation-immersion ultrafiltration, and wherein submerged ultrafiltration is hollow fiber ultrafiltration membrane, and membrane material is polyvinylidene difluoride (PVDF), and membrane pore size is 0.01 micron.The potassium ferrate dosage is 1mg/L, and coagulating agent iron trichloride dosage is 2mg/L (in iron).The immersed type membrane pond of taper slot part, in the cross-sectional height of pond body, heavy mud groove and solid-liquid displacement zone and the aspect ratio of putting the film district are: 4: 1: 1.2.The film operational conditions is: flux is 1.5m/d, move 30 minutes, backwash 1 minute, the backwash water yield is 1.2 times of water production rate, 1/2nd water yields in the heavy mud groove of the cross section taper of discharging membrane cisterna bottom after backwash finishes, immersion system recoveries rate is to be 100 days 95%, the CIP cleaning interval.Adopt common process and common ultrafiltration pond: preliminary sedimentation-coagulating sedimentation-sand filtration-common immersion ultrafiltration, the ultrafiltration rate of recovery are to be 60 days 92%, the CIP cleaning interval.
Embodiment 2
Certain marine site seawater b is adopted in this test, and the water quality situation is as shown in table 2.
Table 2 raw water quality table
| Index | Turbidity (NTU) | COD Mn(mg/L) | pH |
| Raw water quality | 100-150 | 4.3 | 7.8-8.8 |
By as seen from Table 2, raw water quality belongs to III class water body, and water body is polluted.System's operation process is preliminary sedimentation-potassium permanganate oxidation-In-line coagulation-immersion ultrafiltration, and wherein submerged ultrafiltration is hollow fiber ultrafiltration membrane, and membrane material is polyvinylidene difluoride (PVDF), and membrane pore size is 0.01 micron.The potassium permanganate dosage is 1mg/L, and coagulating agent iron trichloride dosage is 1mg/L (in iron).The immersed type membrane pond of taper slot part, in the cross-sectional height of pond body, heavy mud groove and solid-liquid displacement zone and the aspect ratio of putting the film district are: 5: 1: 1.1.The film operational conditions is: flux is 1.2m/d, the siphon water outlet, move 30 minutes, backwash 1 minute, the backwash water yield is 1.1 times of water production rate, / 3rd water yields in the heavy mud groove of the cross section taper of discharging membrane cisterna bottom after backwash finishes, immersion system recoveries rate is to be 140 days 96%, the CIP cleaning interval.The siphon water outlet phase, ton water is saved the 0.031kwh/ ton.
Comparative Examples 1
Certain marine site seawater b is adopted in this test, and the water quality situation is as shown in table 2.
Common process and common ultrafiltration pond are adopted in system operation: preliminary sedimentation-coagulating sedimentation-sand filtration-common immersion ultrafiltration, and wherein submerged ultrafiltration is hollow fiber ultrafiltration membrane, and membrane material is polyvinylidene difluoride (PVDF), and membrane pore size is 0.01 micron.The film operational conditions is: flux is 1.2m/d, and suction pump suction water outlet move 30 minutes, backwash 1 minute, and the backwash water yield is 1.1 times of water production rate, interior all water yields of discharging membrane cisterna after backwash finishes, and immersion system recoveries rate is to be 90 days 92%, the CIP cleaning interval.
Embodiment and Comparative Examples are compared, can find out from Comparative Examples 1, adopt the present invention to process and pollute the marine site seawater, need not the settling tank precipitation after coagulant dosage and directly enter membrane cisterna, reduced the floor space of settling tank and the complicacy of operation; Common immersed type membrane pond does not have solid-liquid displacement zone and heavy mud groove, and general the cleaning finished, rinse water in the blow-down pit body, and the system recoveries rate is low; Adopt the present invention with the immersed type membrane pond of taper slot part, be convenient to utilize the siphon water outlet, energy-saving and cost-reducing.
Claims (7)
1. immersed type membrane pond with the taper slot part, described membrane cisterna comprises pond body (1), water-in and pipeline (2), water port and pipeline (3), water outlet and pipeline (4) and membrane module (5), it is characterized in that: the bottom of pond body (1) is the heavy mud groove of cross section taper, the middle part is solid-liquid displacement zone, and top is for putting the film district; Membrane module is placed in the film district, and water-in is positioned at solid-liquid displacement zone; Water port is positioned at the lowest part of heavy mud groove; Water outlet is positioned at the top of putting the film district.
2. the immersed type membrane pond with the taper slot part according to claim 1 is characterized in that: in the cross-sectional height of pond body, heavy mud groove and solid-liquid displacement zone and the aspect ratio of putting the film district are: (4～8): 1: (1.1～1.4).
3. a right to use requires the sea water desaltination pretreatment process in the pollution marine site of 1 described immersed type membrane pond with the taper slot part, it is characterized in that: comprise following steps:
Pending water enters immersed type membrane pond with the taper slot part by service pump, after this pending water enters solid-liquid displacement zone, the flco of larger particles material and suspension sinks in the mud groove, after the water in upper deployment film district directly filters by membrane module, adopts the suction of siphon or pump to discharge from water outlet.
4. sea water desaltination pretreatment process according to claim 3 is characterized in that: pending water first passes through preoxidation operation and/or coagulation operation before entering immersed type membrane pond with the taper slot part by service pump.
5. sea water desaltination pretreatment process according to claim 4, it is characterized in that: in described preoxidation operation, the preoxidation agent of use is one or more in ozone, potassium permanganate or potassium ferrate.
6. sea water desaltination pretreatment process according to claim 4, it is characterized in that: in described coagulation operation, the coagulating agent of use is one or more in iron trichloride or polymerize aluminum chloride.
7. sea water desaltination pretreatment process according to claim 3 is characterized in that: also contain the film system and regularly generally clean or matting; Described general cleaning step is: adopt ultrafiltration to produce the combined cleaning of the direct backwash of water and air purge, and standing 10-30 minute, open the scupper valve goalkeeper solid-liquid displacement zone of membrane cisterna bottom and the rinse water in heavy mud groove district and discharged by water port, carry out ultra-filtration filters; Matting is first generally to clean, and then membrane module is carried out the combined cleaning of medicament backwash and air purge, and cleaning is carried out ultra-filtration filters after finishing.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104140172A (en) * | 2014-08-14 | 2014-11-12 | 中冶海水淡化投资有限公司 | Seawater desalination pretreatment method |
| CN105800736A (en) * | 2016-04-27 | 2016-07-27 | 浙江净源膜科技股份有限公司 | High-efficiency treatment method and high-efficiency treatment device for oil-containing wastewater |
| WO2017017370A1 (en) * | 2015-07-27 | 2017-02-02 | FONTAINE, Marie-Sully | Methods and apparatus for carrying out the step of desalting food preserved by salting in the best conditions of hygiene and efficacy |
| CN109250840A (en) * | 2018-09-30 | 2019-01-22 | 江苏农林职业技术学院 | A method of black and odorous water is handled using potassium ferrate and activated carbon combined enhanced coagulation |
| 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 |
-
2011
- 2011-11-18 CN CN2011103668410A patent/CN103121760A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104140172A (en) * | 2014-08-14 | 2014-11-12 | 中冶海水淡化投资有限公司 | Seawater desalination pretreatment method |
| CN104140172B (en) * | 2014-08-14 | 2015-12-02 | 中冶海水淡化投资有限公司 | A kind of Seawater desalination pretreatment method |
| WO2017017370A1 (en) * | 2015-07-27 | 2017-02-02 | FONTAINE, Marie-Sully | Methods and apparatus for carrying out the step of desalting food preserved by salting in the best conditions of hygiene and efficacy |
| FR3039362A1 (en) * | 2015-07-27 | 2017-02-03 | Daniel Membrives | METHODS AND EQUIPMENT FOR PERFORMING IN THE BEST CONDITIONS OF EFFICIENCY AND HYGIENE THE DESSALING STEP OF FOOD PRESERVED BY SALAISON. |
| CN105800736A (en) * | 2016-04-27 | 2016-07-27 | 浙江净源膜科技股份有限公司 | High-efficiency treatment method and high-efficiency treatment device for oil-containing wastewater |
| CN109250840A (en) * | 2018-09-30 | 2019-01-22 | 江苏农林职业技术学院 | A method of black and odorous water is handled using potassium ferrate and activated carbon combined enhanced coagulation |
| 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 |
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Application publication date: 20130529 |