CN103153876A - Water-treatment method and desalinization method - Google Patents
Water-treatment method and desalinization method Download PDFInfo
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- CN103153876A CN103153876A CN2011800499103A CN201180049910A CN103153876A CN 103153876 A CN103153876 A CN 103153876A CN 2011800499103 A CN2011800499103 A CN 2011800499103A CN 201180049910 A CN201180049910 A CN 201180049910A CN 103153876 A CN103153876 A CN 103153876A
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- water
- liquid separation
- solid
- separation unit
- dissolved oxygen
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
Abstract
A water-treatment method wherein filtered water, obtained by using a solid-liquid separation unit to perform solid-liquid separation on untreated water having a dissolved-oxygen level of 1 mg/L or greater, is treated using a reverse-osmosis membrane and/or a nanofiltration membrane. Performing gas cleaning, wherein a deoxidizing gas is used to clean the solid-liquid separation unit such that the dissolved-oxygen level of the aforementioned filtered water falls to 0.5 mg/L or below, minimizes biofouling of the reverse-osmosis membrane or nanofiltration membrane, without using chemical additives, when manufacturing high-quality water such as drinking water or industrial water by using a reverse-osmosis membrane or nanofiltration membrane to perform membrane treatment of filtered water obtained by using a solid-liquid separation unit to perform solid-liquid separation on untreated water such as seawater, river water, or post-secondary-treatment sewer water.
Description
Technical field
The present invention relates to process to make the water treatment method of the high-quality water such as tap water, process water through film by the former water (not purifying waste water) of seawater, river, water drain water secondary treatment water etc.
Background technology
As made a kind of method of high-quality water by former water such as seawater, the water treatment method that uses reverse osmosis membrane, nanofiltration membrane to carry out is arranged.Due to the solids component that contains dirt etc. in former water, so directly carry out the situation of membrane filtration at Jiang Yuanshui, be attached to the lip-deep solids component of film and become many, pressure reduction sharply rises.Therefore, need in advance former water to be carried out pre-treatment, the method for the most often using is to add flocculation agent in Xiang Yuanshui, makes the solids component agglomerate, with the cohesion sand filtration method of the filtrations such as sand, hard coal.But the method easily is subject to the impact of former water change, and water quality treatment is unstable, so adopt in recent years the film pre-treatment, processes processed water with secondary filter film, ultra-filtration membrane.
These pre-treatments need regularly will to be deposited in sand through continuing to filter, intermembranous solids component cleans and removes, so usually together with the back-pressure of using filtered water is cleaned, carry out washing out by being blown into air the air purge of solids component.
On the other hand, even removed solids component by aforesaid method, biomembranous on the microbial growth on the face of reverse osmosis membrane, nanofiltration membrane or face adhere to, be that biodeterioration can cause also sometimes that mould is poor sharply to rise, the perviousness of film, separation property variation.As the means that prevent biodeterioration, the whole bag of tricks has been proposed, as the method (patent documentation 1) of adding sterilant, the method (patent documentation 2) that the organism in microbial nutrition source reduces is carried out a biological disposal upon, allowed to become to former water, suppress the method (patent documentation 3) of microbial growth etc. by the raising water temperature, but effect not always enough.
In addition, also proposed to suppress by adjusting redox potential in processed water microorganism propagation, prevent the method for biodeterioration.For example put down in writing in patent documentation 4, by adding off and on the reductive agents such as sodium pyrosulfate, Sulfothiorine, can suppress microbial growth, reduced the poor rising of mould.
The prior art document
Patent documentation
Patent documentation 1: international open WO02/080671 brochure
Patent documentation 2: TOHKEMY 2003-112181 communique
Patent documentation 3: TOHKEMY 2010-058064 communique
Patent documentation 4: TOHKEMY 2007-260638 communique
Summary of the invention
The problem that invention will solve
But the method for record in patent documentation 4, owing to will adding reductive agent, so the additive amount of medicament change is many, not only uneconomical, and the mystery that also has medicine that environment is impacted.
Thereby, the object of the invention is to, for by processed water is carried out solid-liquid separation with solid-liquid separation unit, the water treatment method that resulting filtered water is processed with reverse osmosis membrane or nanofiltration membrane, no longer add medicine, just can suppress the biodeterioration of reverse osmosis membrane, nanofiltration membrane.
Solve the means of problem
The present invention who solves this problem is specific as follows.
(1). a kind of water treatment method, to be that processed water more than 1mg/L carries out solid-liquid separation with solid-liquid separation unit to dissolved oxygen concentration, the water treatment method that resulting filtered water is processed with reverse osmosis membrane and/or nanofiltration membrane, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, make the dissolved oxygen concentration in this filtered water be reduced to below 0.5mg/L.
(2). water treatment method as described in (1), it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making dissolved oxygen concentration in this filtered water is to be total run time over half of solid-liquid separation unit the following time of 0.5mg/L.
(3). a kind of method of making water, to be that processed water more than 1mg/L carries out solid-liquid separation with solid-liquid separation unit to dissolved oxygen concentration, resulting filtered water is processed with reverse osmosis membrane and/or nanofiltration membrane, thereby obtain seeing through the method for making water of water, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making the dissolved oxygen concentration in this filtered water is below 0.5mg/L.
(4). method of making water as described in (3), it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making dissolved oxygen concentration in this filtered water is to be total run time over half of solid-liquid separation unit the following time of 0.5mg/L.
The invention effect
The present invention is by cleaning solid-liquid separation unit with depleted gas, the solids component cleaning that is deposited on solid-liquid separation unit not only can be removed, and in the situation that newly do not add medicine, just can reduce the dissolved oxygen concentration of processed water, reduce the multiplication rate of microorganism, thereby can suppress the biodeterioration of reverse osmosis membrane, nanofiltration membrane.
Description of drawings
Fig. 1 is the general flowchart that shows a routine device of implementing water treatment method of the present invention.
The situation (comparative example 1) that Fig. 2 demonstrated the situation (embodiment 1) of cleaning by depleted gas, clean by air, the cleaning air quantity of depleted gas are less than the situation of embodiment 1 (comparative example 2) and the cleaning that will be undertaken by depleted gas and change by the passing that the cleaning that air carries out merges the dissolved oxygen concentration in filtered water in the situation (comparative example 3) of carrying out.
Embodiment
Water treatment method of the present invention is implemented in following water treatment method: be that processed water more than 1mg/L carries out solid-liquid separation with solid-liquid separation unit with dissolved oxygen concentration, resulting filtered water is processed with reverse osmosis membrane and/or nanofiltration membrane.
As the example of processed water, can list such as seawater, river, lakes and marhshes water, underground water, water drain water secondary treatment water etc., can significantly bring into play owing to implementing effect of the present invention, the dissolved oxygen concentration of preferred processed water is more than 1mg/L.
In addition, although solid-liquid separation unit is to separate the mechanism of removing for the solids components such as dirt that processed water is contained, in the present invention, for the solids component that will be deposited on this solid-liquid separation unit washes, and has the structure of supplying with depleted gas.By like this, can obtain implementation result of the present invention.As the example of concrete solid-liquid separation unit, can list the membrane filter appts that uses secondary filter film, ultra-filtration membrane, and the filtration unit that has been paved with the filter materials such as sand, hard coal.About supplying with the structure of depleted gas, which kind of method all can, the pressure of for example adjusting compressed depleted gas with controller is arranged, then supply to the method for solid-liquid separation unit etc.
In addition, the reverse osmosis membrane that can use in the present invention, nanofiltration membrane, so long as can reduce salt concn, making processed water can be used as tap water, process water, town water etc. gets final product, can use material arbitrarily, for example can list, be consisted of by rhodia class, polyamide-based material.Wherein, effectively consisted of by polyamide-based material especially in the method for the invention.Polyamide-based film is to low as the most normally used chlorine patience of sterilant, and is significantly deteriorated even the chlorine of extremely low concentration also can make film occur, so be difficult to prevent biodeterioration.Thereby implementation result performance of the present invention significantly.
This water treatment method in the present invention, it is characterized in that, carry out cleaning by depleted gas the purge of gas of solid-liquid separation unit, clean and remove the solids component that is deposited on solid-liquid separation unit, the dissolved oxygen concentration that is undertaken in filtered water that solid-liquid separation obtains by described solid-liquid separation unit can be reduced to below 0.5mg/L.
Know, the multiplication rate of microorganism depends on dissolved oxygen concentration, generally defers to following formula.
μ＝μ
max×S
O2/(K
O2＋S
O2)
Wherein, μ: the ratio multiplication rate ［ 1/d ］ of microorganism (specific proliferation rate), μ
max: high specific multiplication rate ［ 1/d ］, S
O2: dissolved oxygen concentration ［ mg/L ］, K
O2: the semi-saturation constant ［ mg/L ］ of dissolved oxygen.
K
O2Value according to the kind of microorganism and different, is generally 0.5 ［ mg/L ］ degree.Thereby, by dissolved oxygen concentration is dropped to below 0.5mg/L, the multiplication rate of microorganism can be reduced to below 1/2.Based on this reason, in the present invention, preferably will be reduced to below 0.5mg/L by the dissolved oxygen concentration that described solid-liquid separation unit carries out in filtered water that solid-liquid separation obtains.Here preferred, setting example as having the dissolved oxygen meter of diaphragm type electrode, is monitored dissolved oxygen concentration in filtering trough, is confirmed whether thus as below 0.5mg/L.Depleted gas is so long as by blowing into solid-liquid separation unit with it in addition, just dissolved oxygen can be driven out of to get final product, and can list such as nitrogen, helium, argon gas etc.Although purge of gas can all carried out always, consider the cost aspect, preferably intermittently carry out.Moreover the dissolved oxygen concentration in preferred filtered water is to be total run time over half of solid-liquid separation unit the following time of 0.5mg/L.Here " total run time of solid-liquid separation unit " refers to the summation of each operation required time of the filtration of solid-liquid separation unit and cleaning, water supply, draining.
Embodiment
The below is described more specifically the present invention, but the present invention is not limited only to this embodiment.
(embodiment 1)
, as processed water processed water 1 use treatment process shown in Figure 1 is processed with seawater (dissolved oxygen concentration 7mg/L).First processed water 1 is put into and be impregnated with separatory membrane 3 (poly-vinylidene fluoride macaroni yarn ultra-filtration membrane processed (the beautiful LSU-1515 processed in east), membrane area: 50m
2) steeping vat 2 (useful capacity: 350L), carry out the filtration of processed water by separatory membrane 3.Filtration is undertaken by sucking pump 4, and filtration flow-rate is made as 1m/d.Next, by conveying pump 6, the core formula strainer 7 (ロ キ テ Network ノ SLS-050 processed) of filtered water 55 μ m from the aperture is passed through, then supply water to reverse osmosis membrane apparatus 9 by high-pressure pump 8, filter, obtain thus seeing through water 10 and condensed water 11.Moreover, as reverse osmosis membrane, use membrane material as polymeric amide, ratio of desalinization be 99.75%, membrane area is 7.8m
2Spiral type reverse osmosis membrane apparatus (the beautiful TM810C processed in east), 7 series connection are turned round.Setting the flow rate of membrane filtra tion during running is 14L/m
2/ hour, the rate of recovery is 37%.Moreover this rate of recovery is calculated by the flow that sees through water 10/(seeing through flow+condensed water 11 flows of water 10) * 100.
The running of separatory membrane 3 is 1 circulation 35 minutes, carries out with step shown in table 1.
Table 1
| Supply water | 2 minutes |
| Nitrogen purge | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+nitrogen purge (+supply water) | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+nitrogen purge (+supply water) | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+nitrogen purge (+supply water) | 1 minute |
| Draining | 2 minutes |
At first, last 2 minutes clockwise steeping vats 2 and supply with processed water 1, after becoming full water state, use nitrogen 12 to clean (air quantity: IOOL/ minute), drive the dissolved oxygen in processed water out of.Next, carry out filtering in 9 minutes.Moreover, water level sensor is set in steeping vat, when reaching low-water level when filtering, can automatic water-supply to full water state.Next, for the solids components such as dirt that will pile up by filtration wash, carry out simultaneously back-pressure and clean and nitrogen purge.It is to make filtered water 5 begin stream with the speed of 52L/ minute from filtering side by backwashing pump 13 that back-pressure is cleaned.Nitrogen purge was carried out with air quantity 100L/ minute in addition.When this operation will finish, also can suitably supply water, become full water state.The operation of cleaning 1 minute with this filtration 9 minutes, is again carried out 3 times repeatedly, and is last for the solids component that will remain in steeping vat is discharged to outside system, carries out draining.This 1 the circulation operation of 35 minutes, turn round repeatedly.
The passing of dissolved oxygen concentration in running, in filtered water 5 changes as shown in Figure 2.In order to supply water in the process of filter progress, although be not always below 0.5mg/L, the time over half of the total run time of solid-liquid separation unit remains on below 0.5mg/L.In addition, although monitoring the pressure difference (hereinafter referred to " running pressure reduction ") of reverse osmosis pleurodiaphragmatic in terspace water and condensed water in the running of reverse osmosis membrane apparatus 9 always, in the running between 2 months, running pressure reduction only is increased to approximately 33kPa slightly from about 30kPa.
(comparative example 1)
Replacement is cleaned and is used air instead and clean with nitrogen, in addition, turns round with the method identical with embodiment 1.The passing of dissolved oxygen concentration in running, in filtered water 5 changes as shown in Figure 2.Dissolved oxygen concentration changes between 7～8mg/L.The running pressure reduction of result, reverse osmosis membrane is had to carry out liquid and is cleaned through the running of 2 months, is raised to approximately lOOkPa from about 30kPa.
(comparative example 2)
In the condition of embodiment 1, the air quantity when making nitrogen purge is 30L/ minute, turns round with the method identical with embodiment 1 in addition.The passing of dissolved oxygen concentration in running, in filtered water 5 changes as shown in Figure 2.Dissolved oxygen concentration is not even be reduced to after nitrogen purge below 0.5mg/L, in approximately 1mg/L change yet.The running of the running pressure reduction of result, reverse osmosis membrane by 2 months, be raised to approximately lOOkPa from about 30kPa, have to carry out liquid and clean.
(comparative example 3)
In 4 cleanings carrying out in the condition of embodiment 1, in 1 circulation in 35 minutes, initial cleaning is cleaned with nitrogen, other 3 cleanings clean to turn round with air.Concrete running step is as shown in table 2.
Table 2
| Supply water | 2 minutes |
| Nitrogen purge | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+air purge (+supply water) | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+air purge (+supply water) | 1 minute |
| Filter (+supply water) | 9 minutes |
| Back-pressure cleaning+air purge (+supply water) | 1 minute |
| Draining | 2 minutes |
The condition identical with embodiment 1 with other condition turns round.The passing of dissolved oxygen concentration in running, in filtered water 5 changes as shown in Figure 2.In 1 circulation (filtration time 27 minutes) of 35 minutes, dissolved oxygen concentration be 0.5mg/L following be only incipient 6 minutes.The running of the running pressure reduction of result, reverse osmosis membrane by 2 months is raised to approximately lOOkPa from about 30kPa, has to carry out liquid and cleans.
The industry utilizability
The present invention can be as carrying out solid-liquid separation by the former water with seawater, river, water drain water secondary treatment water etc. with solid-liquid separation unit, resulting filtered water is carried out film with reverse osmosis membrane or nanofiltration membrane process, thereby the method for making the high-quality water such as tap water, process water is used well.
The drawing reference numeral explanation
1 processed water
2 steeping vats
3 separatory membranes
4 sucking pumps
5 filtered water
6 conveying pumps
7 core formula strainers
8 high-pressure pump
9 reverse osmosis membrane apparatus
10 see through water
11 condensed water
12 nitrogen
13 backwashing pumps
Claims (4)
1. water treatment method, to be that processed water more than 1mg/L carries out solid-liquid separation with solid-liquid separation unit to dissolved oxygen concentration, the water treatment method that resulting filtered water is processed with reverse osmosis membrane and/or nanofiltration membrane, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, make the dissolved oxygen concentration in this filtered water be reduced to below 0.5mg/L.
2. water treatment method as claimed in claim 1, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making dissolved oxygen concentration in this filtered water is to be total run time over half of solid-liquid separation unit the following time of 0.5mg/L.
3. method of making water, to be that processed water more than 1mg/L carries out solid-liquid separation with solid-liquid separation unit to dissolved oxygen concentration, resulting filtered water is processed with reverse osmosis membrane and/or nanofiltration membrane, thereby obtain seeing through the method for making water of water, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making the dissolved oxygen concentration in this filtered water is below 0.5mg/L.
4. method of making water as claimed in claim 3, it is characterized in that, carry out cleaning with depleted gas the purge of gas of solid-liquid separation unit, making dissolved oxygen concentration in this filtered water is to be total run time over half of solid-liquid separation unit the following time of 0.5mg/L.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP243054/2010 | 2010-10-29 | ||
| JP2010243054 | 2010-10-29 | ||
| PCT/JP2011/074617 WO2012057176A1 (en) | 2010-10-29 | 2011-10-26 | Water-treatment method and desalinization method |
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| CN103153876A true CN103153876A (en) | 2013-06-12 |
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| JP (1) | JPWO2012057176A1 (en) |
| CN (1) | CN103153876A (en) |
| WO (1) | WO2012057176A1 (en) |
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| CN112646975A (en) * | 2020-12-17 | 2021-04-13 | 紫金矿业集团股份有限公司 | Treatment method for reducing and recycling copper ore acid raffinate |
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| CN110240300B8 (en) * | 2019-06-26 | 2021-09-28 | 山东奥士康新材料科技有限公司 | Water purification unit with multilayer nanofiltration membrane |
| NL2027905B1 (en) * | 2021-04-01 | 2022-10-17 | Allied Waters B V | A method for producing tailored quality water. |
Citations (2)
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|---|---|---|---|---|
| CN1408653A (en) * | 2002-09-24 | 2003-04-09 | 天津大学 | Producing process and technology for electronic grade water by intergrated film process |
| CN201305523Y (en) * | 2008-11-12 | 2009-09-09 | 恩那社(上海)水处理系统有限公司 | Processing system for transforming normal water to ultrapure water |
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| JP2680855B2 (en) * | 1988-09-30 | 1997-11-19 | 日東電工株式会社 | How to operate the hollow fiber membrane module |
| US7318894B2 (en) * | 2001-08-29 | 2008-01-15 | Graham John Gibson Juby | Method and system for treating wastewater |
| DE602007008848D1 (en) * | 2006-03-16 | 2010-10-14 | Shell Int Research | METHOD AND DEVICE FOR REMOVING METAL SULFIDE PARTICLES FROM A LIQUID CURRENT |
| JP2008183510A (en) * | 2007-01-30 | 2008-08-14 | Toray Ind Inc | Purified water production method and apparatus |
| JP5581578B2 (en) * | 2008-09-16 | 2014-09-03 | 三菱レイヨン株式会社 | Membrane cleaning device, membrane separation device, and wastewater treatment device |
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- 2011-10-26 JP JP2012511469A patent/JPWO2012057176A1/en active Pending
- 2011-10-26 WO PCT/JP2011/074617 patent/WO2012057176A1/en active Application Filing
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1408653A (en) * | 2002-09-24 | 2003-04-09 | 天津大学 | Producing process and technology for electronic grade water by intergrated film process |
| CN201305523Y (en) * | 2008-11-12 | 2009-09-09 | 恩那社(上海)水处理系统有限公司 | Processing system for transforming normal water to ultrapure water |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112646975A (en) * | 2020-12-17 | 2021-04-13 | 紫金矿业集团股份有限公司 | Treatment method for reducing and recycling copper ore acid raffinate |
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| WO2012057176A1 (en) | 2012-05-03 |
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