CN102198986A - Method for improving water yield of membrane system by refluxing membrane backwashing water - Google Patents
Method for improving water yield of membrane system by refluxing membrane backwashing water Download PDFInfo
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- CN102198986A CN102198986A CN 201110094872 CN201110094872A CN102198986A CN 102198986 A CN102198986 A CN 102198986A CN 201110094872 CN201110094872 CN 201110094872 CN 201110094872 A CN201110094872 A CN 201110094872A CN 102198986 A CN102198986 A CN 102198986A
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- molysite
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- 239000012528 membrane Substances 0.000 title claims abstract description 99
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000011001 backwashing Methods 0.000 title claims description 61
- 238000010992 reflux Methods 0.000 title claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 16
- 238000001471 micro-filtration Methods 0.000 claims abstract description 13
- 238000002203 pretreatment Methods 0.000 claims abstract description 13
- 238000005345 coagulation Methods 0.000 claims abstract description 11
- 230000015271 coagulation Effects 0.000 claims abstract description 11
- 239000002245 particle Substances 0.000 claims abstract description 8
- 238000005273 aeration Methods 0.000 claims abstract description 7
- 238000004140 cleaning Methods 0.000 claims abstract description 7
- 239000002957 persistent organic pollutant Substances 0.000 claims abstract description 5
- 238000001179 sorption measurement Methods 0.000 claims abstract description 4
- 239000006228 supernatant Substances 0.000 claims abstract description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 33
- 238000006243 chemical reaction Methods 0.000 claims description 18
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 230000035484 reaction time Effects 0.000 claims description 8
- 238000005374 membrane filtration Methods 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 239000003610 charcoal Substances 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 3
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 2
- 230000000694 effects Effects 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 13
- 150000002505 iron Chemical class 0.000 abstract description 6
- 239000005416 organic matter Substances 0.000 abstract description 4
- 238000013019 agitation Methods 0.000 abstract description 2
- 238000002156 mixing Methods 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000004062 sedimentation Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 12
- 239000002352 surface water Substances 0.000 description 12
- 235000020188 drinking water Nutrition 0.000 description 10
- 239000003651 drinking water Substances 0.000 description 10
- 230000004907 flux Effects 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000004576 sand Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000008399 tap water Substances 0.000 description 3
- 235000020679 tap water Nutrition 0.000 description 3
- 241000195493 Cryptophyta Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000005422 algal bloom Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000001717 pathogenic effect Effects 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003053 toxin Substances 0.000 description 1
- 231100000765 toxin Toxicity 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本发明公开了一种膜反洗水回流提高膜系统产水率方法。采用铁盐混凝和活性炭吸附对膜反洗水进行预处理，将预处理过的膜反洗水上清液回流至调节池与水厂清洁水混合后再进入系统对超滤膜或微滤膜进行清洗，其具体预处理方法由以下步骤完成：向预处理反应器中投加铁盐；向预处理反应器中投加粉末活性炭；铁盐和粉末活性炭投加量根据反洗水中的有机物含量确定；预处理反应器以曝气方式提供搅拌混合，使铁盐和粉末活性炭与反洗水中的有机污染物充分反应，形成的铁盐絮凝体和粉末活性炭颗粒通过沉淀去除，使膜反洗水回流至膜系统时不会影响膜出水水质。本发明能够降低膜反洗水中的有机物含量，有效地提高膜处理系统的回收率。
The invention discloses a method for increasing the water production rate of a membrane system by backflowing membrane backwash water. The membrane backwash water is pretreated by iron salt coagulation and activated carbon adsorption, and the supernatant of the pretreated membrane backwash water is returned to the adjustment tank and mixed with the clean water of the water plant before entering the system for ultrafiltration or microfiltration membranes Cleaning, the specific pretreatment method is completed by the following steps: dosing iron salt into the pretreatment reactor; adding powdered activated carbon to the pretreatment reactor; the dosage of iron salt and powdered activated carbon is based on the organic matter content in the backwash water Confirm; the pretreatment reactor provides agitation and mixing in the form of aeration, so that the iron salt and powdered activated carbon can fully react with the organic pollutants in the backwash water, and the formed iron salt flocs and powdered activated carbon particles are removed by sedimentation, so that the membrane backwash water When it is returned to the membrane system, it will not affect the quality of the membrane effluent. The invention can reduce the content of organic matter in the membrane backwash water and effectively improve the recovery rate of the membrane treatment system.
Description
Technical field
The invention belongs to water technology, be specifically related to a kind of technological method that utilizes again that membrane backwashing is recycled.
Background of invention
Safety of drinking water is most important to HUMAN HEALTH, but aggravation along with pollution of waterhead, the appearance of problems such as algae toxin that the pathogenic protozoon in the water body " two worms ", algal bloom cause and disinfection byproduct (DBP) makes tradition can not satisfy the requirement of the drinking water quality standard of increasingly stringent for water technology.Membrane separating method is considered to prepare now one of high-quality and safety tap water important techniques means, and gains universal acceptance.Advantages such as ultrafiltration and micro-filtration technology are low because of working pressure, stable effluent quality have the potentiality that replace traditional handling technology of water supply, have become the membrane technique that is most widely used.But ultra-filtration membrane and microfiltration membrane are in operational process, because the pollutent that is trapped, forms cake layer in the continuous accumulation on film surface and cause transmembrane pressure (TMP) to increase or membrane flux reduces.For guaranteeing the steady running of film system, need regularly membrane module to be carried out backwash, this will consume a large amount for the treatment of water, cause the rate of recovery of system to reduce, and this part backwash water abbreviates membrane backwashing as.Especially in temperature in winter lower period, along with the reduction water body viscosity of water temperature increases, pilot scale film system can adopt usually and reduce flux and the steady running of system is kept in frequent back flushing, and makes producing water ratio lower.Therefore, how the efficient recovery membrane backwashing is the problem that ultrafiltration or micro-filtration technology must solve in drinking water treatment is used to improve system's producing water ratio and to reduce cost.
The recovery of membrane backwashing has two kinds of schemes: scheme one is the device of newly-built special disposal backwash water; Scheme two is the equalizing tanks that backwash water directly are back to water factory, and enters membrane filtration system again after former water mixes.Employing scheme one need be built one in addition and be overlapped independently membrane backwashing recovery and processing system, and it is complicated to increase investment and operational management; Employing scheme two, the pollutent that washes in the film backwash process can cause the pollution of the former water of water factory, and after reentering the film system, certainly will increase dosage and film and pollute speed.Under this background, take all factors into consideration the relative merits of above two kinds of recovery schemes, trial is at first carried out pre-treatment to membrane backwashing, pollutent in the membrane backwashing is converted into solid phase to be removed by sludge settling, pre-treatment effluent recycling to the equalizing tank of water factory is mixed with former water, so both can avoid the expensive problem of newly-built membrane backwashing recovery system, the film that has caused when having solved direct the backflow again pollutes aggravation.
Summary of the invention
The objective of the invention is, provide a kind of membrane backwashing is recycled the method for utilizing again, to improve film system producing water ratio.
Membrane backwashing refluxes and improves film system producing water ratio method, adopt molysite coagulation and charcoal absorption that membrane backwashing is carried out pre-treatment, enter system again after pretreated membrane backwashing supernatant liquor is back to equalizing tank and the water factory cleaning water is mixed ultra-filtration membrane or microfiltration membrane are cleaned, its concrete pretreatment process is finished by following steps:
When (1) treating that membrane backwashing enters the pretreatment reaction device, in the pretreatment reaction device, add molysite, reaction times 10～20min;
(2) in the pretreatment reaction device, add Powdered Activated Carbon then, reaction times 30～40min;
(3) described molysite and Powdered Activated Carbon dosage are determined according to the organic content in the backwash water, when the permanganate index in the membrane backwashing is 5.0+0.5mg/L, the reference value of molysite dosage is 15mg/L, and the reference value of Powdered Activated Carbon dosage is 10mg/L; If treatment effect is not good, can increase by 30% the molysite and the dosage of Powdered Activated Carbon;
(4) the pretreatment reaction device provides with stirring and aeration mode and mixes, make molysite and Powdered Activated Carbon can with the abundant contact reacts of the organic pollutant in the membrane backwashing, molysite flocs unit that forms and Powdered Activated Carbon particle are removed by precipitation, reach the purpose of purifying membrane backwashing.
Membrane backwashing is meant the waste water that the membrane module of ultra-filtration membrane or microfiltration membrane is carried out backwash or cleaning.
Molysite is meant iron(ic) chloride or ferric sulfate or poly-ferric chloride or bodied ferric sulfate.
Powdered Activated Carbon is meant that particle diameter has the porousness charcoal of adsorption function less than 0.1mm, and its outward appearance is Powdered.
If the small organic molecule content in the membrane backwashing is less, in the pretreatment reaction device, after the molysite coagulation process is handled, in the time of can satisfying the water quality requirement of water factory's cleaning water, can not add Powdered Activated Carbon.
Beneficial effect of the present invention is: in giving water treatment, the present invention adopts membrane backwashing is back to equalizing tank after molysite coagulation and charcoal absorption pre-treatment, can not impact film system effluent quality, make it the requirement of satisfied " drinking water sanitary standard ", effectively improved the rate of recovery of water treatment system, significant to alleviating the increasingly serious water resources imbalance between supply and demand of China.This method level of automation height, simple to operation, working cost is low, can be generalized to the water factory that adopts conventional treatment process, has broad application prospects.
Description of drawings
Shown in accompanying drawing be the experimental installation system diagram of the embodiment of the invention.
Embodiment
Below by specific embodiment method steps of the present invention is described further.Present embodiment is narrative simultaneously, is not determinate, can not limit protection scope of the present invention with this.
Membrane backwashing refluxes and improves film system producing water ratio method, and membrane backwashing is meant the waste water that the membrane module of ultra-filtration membrane or microfiltration membrane is carried out backwash or cleaning.Present embodiment utilizes molysite coagulation-micro-filtration processing simulation Drinking Water preparation system to carry out (seeing accompanying drawing).Membrane backwashing among the present invention is promptly from water treatment system.The every 30min of hollow fiber film assembly that is used for water treatment micro-filtration technology carries out a backwash, to recover the flux of ultra-filtration membrane.What molysite adopted is iron(ic) chloride; What Powdered Activated Carbon adopted is the porousness charcoal of particle diameter less than 0.1mm.
The present invention's pre-treatment that can reflux to the membrane backwashing of two kinds of water technologies.
The recovery of embodiment 1. precipitation-ultrafiltration technology membrane backwashings
Organic molecular weight distribution sees attached list 1 in the membrane backwashing, this part organism mainly is distributed in molecular weight greater than (Da is a molecular weight unit in 30kDa and the interval less than 1kDa, dalton), dissolved organic carbon (DOC) in these two intervals accounts for 44.2% and 30.8% of total organic matter DOC value respectively, and the visible pretreated emphasis of membrane backwashing is the organism in these two intervals.
According to the concrete pretreatment process step of membrane backwashing:
When (1) treating that membrane backwashing enters the pretreatment reaction device, add the iron(ic) chloride of 20mg/L in the pretreatment reaction device, the reaction times is 20min.
(2) add Powdered Activated Carbon 10mg/L (hereinafter to be referred as PAC) then in the pretreatment reaction device, the reaction times is 30min.
(3) the permanganate index mean value in the membrane backwashing is 3.5mg/L in the present embodiment.
(4) the pretreatment reaction device provides with aeration mode and mixes, make molysite and Powdered Activated Carbon can with the abundant contact reacts of the organic pollutant in the membrane backwashing, the molysite flocs unit of formation and Powdered Activated Carbon particle are removed by precipitation.
The embodiment test-results shows: after molysite coagulation-PAC absorption pre-treatment, and the average COD of membrane backwashing
MnCan be reduced to 2.2～2.5mg/L by 2.3～5.4mg/L, DOC mean value is reduced to 3.15mg/L by 3.89mg/L simultaneously.
Membrane backwashing after the processing refluxes, and can not cause tangible influence to film system effluent quality.Be mixed in proportion with natural surface source water and obtain the water that is mixed as the former water of water factory; Be mixed water after coagulation-microfiltration membrane system is handled, and the natural surface water after its water quality and the processing does not have evident difference (seeing attached list 2), and all satisfies the requirement of " drinking water sanitary standard " (GB 5749-2006).
The membrane backwashing of embodiment 1 can bring up to 98.8% by original 88.2% with the rate of recovery of Drinking Water treatment system after pre-treatment is reclaimed.
The recovery of embodiment 2. sand filtrations-ultrafiltration technology membrane backwashing
Organic molecular weight distribution sees attached list 3 in the membrane backwashing, this part organism mainly is distributed in molecular weight greater than in 30kDa and the interval less than 1kDa, DOC accounts for 54.1% and 28.4% of total organic matter DOC value respectively in these two intervals, compare with the natural surface water source, molecular weight significantly reduces between the organic content of 30-3kDa in the membrane backwashing; Molecular weight obviously raises greater than the organic content of 30kDa, and its content is 5.9 times of earth surface water source, and molecular weight is not remarkable less than organism in the 1kDa interval and earth surface water source difference.
The pretreatment technology that adopts is identical with embodiment 1 method.
The embodiment test-results shows: work as FeCl
3Dosage be 15mg/L, the reaction times is 20min; The dosage of PAC is 10mg/L, and the reaction times is 30min.After molysite coagulation-PAC absorption pre-treatment, the average COD of backwash water
MnCan be reduced to 1.6～2.2mg/L by 2.1～5.5mg/L, DOC mean value is reduced to 3.3mg/L by 4.2mg/L simultaneously.
After membrane backwashing adsorbed pre-treatment by molysite coagulation-PAC, organic concentration decreased, and its effluent quality is better than earth surface water source.This shows, the membrane backwashing after the inventive method is handled with enter the film system once more after earth surface water source mixes, can not cause tangible influence to the film effluent quality.The result of example laboratory shows that also backwash water is through FeCl
3Obtain the water that is mixed with mixing with the earth surface water source water of water factory after the PAC pre-treatment, this is mixed water again after molysite coagulation-microfiltration systems is handled, do not have evident difference (seeing attached list 4) with the effluent quality of earth surface water source water after film is handled, and all satisfy " drinking water sanitary standard " requirement (GB5749-2006).
Membrane backwashing among the embodiment 2 can bring up to 99.2% by original 91.8% with the rate of recovery of Drinking Water treatment system after pre-treatment is reclaimed.As seen this method can improve the rate of recovery of water treatment system.
The specific operation process of embodiment: under programmable logic controller (PLC) control, lift pump 1 adds pretreatment reaction device 2 with membrane backwashing, in the pretreatment reaction device, add molysite and PAC again, aeration continuously stirring through gas blower 3, molysite is hydrolyzed in the pretreatment reaction device, coagulation produces flocs unit, continues reaction with larger molecular organics in the membrane backwashing (suspended substance and colloid) and generates the bigger alumen ustum of size; Small organic molecule in the while PAC adsorption film backwash water, molysite flocs unit and PAC particle are discharged the pretreatment reaction device by precipitation, thereby reach the purpose of removing organic pollutant in the membrane backwashing.
The former water of membrane backwashing after the processing and water factory obtains the water that is mixed after by 1: 9 mixed, is used to prepare Drinking Water then.The water that is about to be mixed is stored in the water tank 4; To be mixed respectively water and molysite (test-results that dosage is seen below) of lift pump 5 and volume pump 6 adds coagulation reactor 7, forms flocs unit behind the iron salt hydrolysis coagulation, flows into membrane separation apparatus 8.Larger molecular organics further reacts and generates larger-size alumen ustum in the molysite flocs unit and the water that is mixed, and flocs unit is trapped in the membrane separation apparatus by hollow-fibre membrane 9; Water after the processing collects after going out water pump 10 suctions and is used for water quality detection.Coagulation reactor adopts agitator 11 or aeration to stir, and membrane separation apparatus adopts aeration agitation, and air is provided by gas blower 12.
Organic molecular weight distribution in subordinate list 1 (embodiment 1) precipitation-ultrafiltration technology membrane backwashing
Subordinate list 2 (embodiment 1) surface water and based on the tap water of the water preparation of being mixed of precipitation-ultrafiltration membrane system
Organic molecular weight distribution relatively in subordinate list 3 (embodiment 2) sand filtration-ultrafiltration technology membrane backwashing and the surface water
Annotate: R
DOCRatio for membrane backwashing DOC and earth surface water source water DOC.
Subordinate list 4 (embodiment 2) surface water and based on the tap water of the water preparation of being mixed of sand filtration-ultrafiltration membrane system
Membrane backwashing refluxes and improves the method for film system producing water ratio, and coagulation is fit to remove larger molecular organics, and Powdered Activated Carbon (PAC) can adsorb small organic molecule.With coagulation and PAC absorption coupling, pretreated membrane backwashing is back to water factory's equalizing tank, working cost is low, and is simple to operation, is a kind of very method of practical raising film system producing water ratio.
Claims (4)
1. membrane backwashing refluxes and improves film system producing water ratio method, it is characterized in that adopting molysite coagulation and charcoal absorption that membrane backwashing is carried out pre-treatment, enter system again after pretreated membrane backwashing supernatant liquor is back to equalizing tank and the water factory cleaning water is mixed ultra-filtration membrane or microfiltration membrane are cleaned, its concrete pretreatment process is finished by following steps:
When (1) treating that membrane backwashing enters the pretreatment reaction device, in the pretreatment reaction device, add molysite; Reaction times is 10～20min;
(2) add Powdered Activated Carbon then in the pretreatment reaction device, the reaction times is 30～40min;
(3) described molysite and Powdered Activated Carbon dosage are determined according to the organic content in the backwash water, when the permanganate index in the membrane backwashing is 5.0 ± 0.5mg/L, the reference value of molysite dosage is 15mg/L, and the reference value of Powdered Activated Carbon dosage is 10mg/L; If treatment effect is not good, can increase by 30% the molysite and the dosage of Powdered Activated Carbon;
(4) the pretreatment reaction device provides with stirring and aeration mode and mixes, make molysite and Powdered Activated Carbon can with the abundant contact reacts of the organic pollutant in the membrane backwashing, molysite flocs unit that forms and Powdered Activated Carbon particle are removed by precipitation, reach the purpose of purifying membrane backwashing.
2. reflux according to the described membrane backwashing of claim 1 and improve film system producing water ratio method, described membrane backwashing is meant the waste water that the membrane module of ultra-filtration membrane or microfiltration membrane is carried out backwash or cleaning.
3. reflux according to the described membrane backwashing of claim 1 and improve film system producing water ratio method, it is characterized in that described molysite is meant iron(ic) chloride or ferric sulfate or poly-ferric chloride or bodied ferric sulfate.
4. reflux according to the described membrane backwashing of claim 1 and improve film system producing water ratio method, it is characterized in that described Powdered Activated Carbon is meant that particle diameter has the porousness charcoal of adsorption function less than 0.1mm, its outward appearance is Powdered.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103803742A (en) * | 2013-12-31 | 2014-05-21 | 许昌学院 | Microfiltration water inlet ultrafine powder activated carbon pretreatment method |
| CN109133433A (en) * | 2018-10-17 | 2019-01-04 | 清华大学 | A kind of organic dirty blocking control method of reverse osmosis membrane |
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| CN101786689A (en) * | 2010-02-10 | 2010-07-28 | 厦门市威士邦膜科技有限公司 | Membrane separation concentrated water treatment method and integral coupling device |
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2011
- 2011-04-15 CN CN 201110094872 patent/CN102198986A/en active Pending
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| CN2670352Y (en) * | 2003-12-25 | 2005-01-12 | 曲艳春 | Waste water treating and reusing devices |
| CN101139143A (en) * | 2007-08-14 | 2008-03-12 | 天津市华宇膜技术有限公司 | Hyperfiltration reverse- rinsing water recovery processing method and device thereof |
| CN201080449Y (en) * | 2007-08-14 | 2008-07-02 | 天津市华宇膜技术有限公司 | Hyperfiltering backwashing water recovery device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103803742A (en) * | 2013-12-31 | 2014-05-21 | 许昌学院 | Microfiltration water inlet ultrafine powder activated carbon pretreatment method |
| CN103803742B (en) * | 2013-12-31 | 2016-02-10 | 许昌学院 | Micro-filtration water inlet ultra-micro powder Activated Carbon Pretreatment method |
| CN109133433A (en) * | 2018-10-17 | 2019-01-04 | 清华大学 | A kind of organic dirty blocking control method of reverse osmosis membrane |
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Application publication date: 20110928 |