CN200945417Y - Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution - Google Patents
Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution Download PDFInfo
- Publication number
- CN200945417Y CN200945417Y CN 200620088240 CN200620088240U CN200945417Y CN 200945417 Y CN200945417 Y CN 200945417Y CN 200620088240 CN200620088240 CN 200620088240 CN 200620088240 U CN200620088240 U CN 200620088240U CN 200945417 Y CN200945417 Y CN 200945417Y
- Authority
- CN
- China
- Prior art keywords
- links
- heat exchanger
- reverse osmosis
- osmosis membrane
- export
- 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 - Lifetime
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution, belonging to an ion-exchange membrane caustic soda process device. The bottom of a dilute salt solution head tank is connected with the heat exchanger via dilute salt solution transfer pump; the heat exchanger is connected with an active carbon filter; the active carbon filter is connected with a safety filter; the safety filter is connected with a modified reverse osmosis membrane filter; the concentrated solution outlet end of the modified reverse osmosis membrane filter is connected with a concentrated solution pot, the concentrated solution outlet end of the concentrated solution pot is connected with the heat exchanger, the outlet end of the heat exchanger is connected with the top end of the nitre deposit tank, the nitre deposit tank is connected with a centrifugal machine underneath, the device concentrates the sodium sulfate in the dilute salt solution by the modified reverse osmosis membrane, and then separates the sodium sulfate from the sodium chloride by freezing method to thoroughly deprive of the sodium sulfate accumulated in the chlorine alkali production to balance the sodium sulfate content in the light salt water to make the light salt water meet the electrolysis demand so as to enhance the quality and the stabilization of the light salt waters.
Description
Technical field
The utility model provides a kind of device that ion film caustic soda is produced, especially a kind of device that removes sulfate radical in the light salt brine of being used for.
Background technology
In ion film caustic soda is produced, be that crude salt (NaCl) is dissolved into saturated brine, carry out electrolysis production again and go out products such as NaOH and chlorine.If contain excessive Ca in the salt solution
2+, Mg
2+, SO
4 2-Deng divalent ion impurity, cation can damage and be enhanced fiber on the ionic membrane and center on " window " zone, and anion then can damage the fortifying fibre on the ionic membrane, and in the electrolytic process side reaction can take place, so must remove above impurity before electrolysis.The method of existing salt solution sulfate radical mainly contains barium chloride sulfate radical, calcium chloride sulfate radical, ion-exchange sulfate radical, NF membrane sulfate radical etc.It is the barium chloride sulfate radical that domestic chlor-alkali enterprise uses the most general, and its device mainly is made up of barium chloride dissolving tank, delivery pump, settling tank, filter press etc.The shortcoming of this device mainly is, after adding barium salt in the salt solution, unreacted barium ions is trapped in the salt solution, ionic membrane is caused new harm, remote-effects current efficiency and ionic membrane service life, and the barium sulfate precipitate that generates easily brings the primary brine filtration system into, causes micro-filtration membrane seriously to stop up, and is difficult to remove.Ion-exchange sulfate radical technology is some company's exploitations of Japan, because the metal oxide slurries that use are relatively more expensive, also causes ionic soil in addition easily, does not therefore see the producer of this technology of use at home.NF membrane sulfate radical device mainly contains pretreatment procedure, membrane filtration operation, it is unstable that the disadvantage of this device is exactly the control of pretreatment procedure pH value, cause the NF membrane hydrolysis of membrane filtration operation easily, secondly the operating pressure of membrane filtration operation is too high, causes the compacting of film easily, causes the shortening of membrane lifetime, this technology does not have postprocessing working procedures in addition, therefore cause a large amount of sodium chloride dischargings, cause a large amount of wastes, also incompatibility environmental protection requirement more and more.
Summary of the invention
Technical problem to be solved in the utility model is to provide a kind of modification reverse osmosis membrane apparatus that is used for removing the light salt brine sulfate radical, to remove the sulfate radical in the salt solution, the quality and the stability of raising salt solution, reduction operating cost.
The utility model is to realize like this, be used for removing the modification reverse osmosis membrane apparatus of light salt brine sulfate radical, it has the light salt brine head tank, the bottom of light salt brine head tank is connected with the light salt brine delivery pump, light salt brine carries delivery side of pump to link to each other with the heat exchanger entrance point, the port of export of heat exchanger links to each other with the entrance point of active carbon filter, the port of export of active carbon filter links to each other with the entrance point of security personnel's filter, the port of export of security personnel's filter links to each other by the entrance point of pump with modification reverse osmosis membrane filtration device, the concentrated solution outlet end of modification reverse osmosis membrane filtration device links to each other with concentrated flow container, concentrating the flow container port of export links to each other with the concentrate delivery pump, the port of export of concentrate delivery pump links to each other with heat exchanger, the port of export of heat exchanger links to each other with the entrance point of another heat exchanger, the port of export of heat exchanger links to each other with the upper end of saltpetre sinking device, the upper end of saltpetre sinking device also links to each other with the clear liquid jar, the outlet of clear liquid jar links to each other with the clear liquid delivery pump, the port of export that cleans delivery pump links to each other with heat exchanger, and the bottom of saltpetre sinking device links to each other with centrifuge.
Adopt the modification reverse osmosis membrane of said structure to remove the nitre device, can carry out that the pH value is regulated and temperature control, free chlorine are controlled at pretreatment procedure to light salt brine, utilize the modification reverse osmosis membrane the sodium sulphate enrichment method in the light salt brine in modification reverse osmosis membrane filtration operation, pass through postprocessing working procedures at last, utilize freezing method that sodium chloride and sodium sulphate are separated, and then thoroughly remove the accumulation problem of sodium sulphate in the whole chlor-alkali production, make the mesohalobic sodium sulphate of chlor-alkali production reach balance, satisfy the requirement that salt solution advances electric slot device.The light salt brine that this device is particularly useful in the ion film caustic soda production removes sulfate radical.Compare with existing apparatus, this device has following advantage:
1, in the subtractive process without chemical reaction (because of not using chemical agent), do not produce solid shape discarded object, simplified running management, equipment is easy to installation and is connected, operating maintenance convenient.
2, primary brine quality and the stability of handling through this device thereof obviously is better than existing apparatus, and the sodium sulphate index is controlled at below the 4g/l in the primary brine, Ba in the secondary brine
2+Index is about 2ppb.
3, this device applicability is strong, can different film compound modes be set according to the device needs, but so poor crude salt of chlor-alkali enterprise service property (quality), thereby reduced production cost, the operating cost aspect, this device can be the user every year and saves millions of even up to ten million expenses not as good as 1/5 of existing apparatus.
4, this installs and squeezes into the salt dissolving tank of primary brine system by pump after salt solution after all heat exchange and pump cooling water enter the ground lower storage reservoir, thereby has realized sewage zero-discharge, and effects of energy conservation and environmental protection is good.
Description of drawings
Fig. 1 is the schematic diagram of the utility model to the structure of concentrate generation.
Fig. 2 is the schematic diagram of the structure after the utility model concentrate produces.
Among the figure, 1-light salt brine head tank, 2-light salt brine delivery pump, 3-heat exchanger, 4-active carbon filter, the 5-filter of ensuring public security, 6-modification reverse osmosis membrane filtration device, the 7-cleaning device, 8-concentrates flow container, 9-concentrate delivery pump, 10-heat exchanger, 11-saltpetre sinking device, 12-clear liquid jar, 13-clear liquid delivery pump, another heat exchanger of 14-, the 15-centrifuge, 16-packs outlet, 17-ground lower storage reservoir.
The specific embodiment
The embodiment that provides below in conjunction with accompanying drawing illustrates structure of the present utility model and operation principle.
As shown in drawings, the modification reverse osmosis membrane apparatus that is used for removing the light salt brine sulfate radical of the utility model, it has light salt brine head tank (1), the bottom of light salt brine head tank is connected with light salt brine delivery pump (2), light salt brine carries delivery side of pump to link to each other with heat exchanger (3) entrance point, the port of export of heat exchanger (3) links to each other with the entrance point of active carbon filter (4), the port of export of active carbon filter links to each other with the entrance point of security personnel's filters (5), the port of export of security personnel's filter links to each other by the entrance point of pump with modification reverse osmosis membrane filtration device (6), the concentrated solution outlet end of modification reverse osmosis membrane filtration device links to each other with concentrated flow container (8), concentrating the flow container port of export links to each other with concentrate delivery pump (9), the port of export of concentrate delivery pump links to each other with heat exchanger (10), the port of export of heat exchanger (10) links to each other with the entrance point of another heat exchanger (14), the port of export of another heat exchanger (14) links to each other with the upper end of saltpetre sinking device (11), the upper end of saltpetre sinking device also links to each other with clear liquid jar (12), the outlet of clear liquid jar links to each other with clear liquid delivery pump (13), the port of export that cleans delivery pump links to each other with heat exchanger (10), and the bottom of saltpetre sinking device links to each other with centrifuge (15).
The pipeline that was connected between above-mentioned each parts connects to be realized.
Packing outlet (16) is positioned at the outlet below of solid formation of the bottom of centrifuge (15).
Operation principle of the present utility model is: will be driven into the light salt brine head tank by pump from the light salt brine of electrolysis with ion-exchange film operation, and add NaOH in the import of light salt brine delivery pump then and regulate pH value to 3～6, and remove free chlorine.Temperature drops to 35～50 ℃ after light salt brine process heat exchanger (3) heat exchange after the dechlorination, light salt brine enters active carbon filter, the effect of active carbon mainly is the residual free chlorine of absorption, to prevent that free chlorine from damaging the modification reverse osmosis membrane, the light salt brine that comes out from active carbon filter enters security personnel's filter (5), and security personnel's filter filters and can prevent that big particle from entering modification reverse osmosis membrane filtration operation.From the light salt brine that comes out of security personnel's filter through the pump pressurization after, enter modification reverse osmosis membrane filtration device.Behind the reverse osmosis membrane process physics and chemical method modification on the modification reverse osmosis membrane filtration device, can carry out selective filter to the ion in the light salt brine.There is charged group in the modification reverse osmosis membrane, and these charged groups can optionally repel as SO
4 2-Deng multivalent anions, but it can not separate out picture Cl from feedstock solution
-, ClO
3 -The same monovalention.Like this, sodium chloride in the light salt brine and water can become penetrating fluid and send to salt dissolving tank by the modification reverse osmosis membrane, and SO
4 2-The reverse osmosis membrane that is modified repels concentrated (SO in the concentrate
4 2-Concentration according to charging SO
4 2-Change in concentration and change, scope is at 20g/l～100g/l), the SO of concentrate
4 2-Discharge when concentration reaches finite concentration and enter postprocessing working procedures and handle.The concentrate that comes out from modification reverse osmosis membrane filtration operation enters the concentrate jar by adding after NaOH is regulated the pH value, squeeze into heat exchanger (10) by concentrate pump then, another heat exchanger (14), in these two heat exchangers, carry out heat exchange with-10～-20 ℃ cool brine or other refrigerant that is lower than this temperature, enter saltpetre sinking device at last, temperature in the saltpetre sinking device is controlled at suitable temperature (5～-8 ℃), most like this sodium sulphate will be deposited on the bottom of saltpetre sinking device with the form of sal glauberi, the sal glauberi that comes out from saltpetre sinking device bottom by centrifuge centrifugal after, become the sal glauberi product, enter packing outlet (16), can after packing, sell.The clear liquid that comes out in saltpetre sinking device top enters the clear liquid jar.
Because very low from solid suspension SS in the light salt brine of electrolysis with ion-exchange film operation and bivalent cation content, and SO
4 2-Content is the highest, therefore to the SO in the light salt brine of electrolysis with ion-exchange film operation
4 2-Remove, can improve the efficient of modification reverse osmosis membrane filtration.
The port of export of cleaning device (7) also links to each other with the entrance point of modification reverse osmosis membrane filtration device, does not use cleaning device when normally driving, and only uses when the start-stop car.The effect of cleaning device is to store pure water and configuration cleaning fluid, after reverse osmosis membrane uses a period of time it is cleaned.
This installs salt solution and the whole inflow places of pump cooling water lower storage reservoirs (17) after all heat exchange, can play the water distribution jar of past primary brine operation by pump then.
Heat exchanger (3) can be two that are cascaded.
Claims (1)
1, be used for removing the modification reverse osmosis membrane apparatus of light salt brine sulfate radical, it is characterized in that, it has light salt brine head tank (1), the bottom of light salt brine head tank is connected with light salt brine delivery pump (2), light salt brine carries delivery side of pump to link to each other with heat exchanger (3) entrance point, the port of export of heat exchanger (3) links to each other with the entrance point of active carbon filter (4), the port of export of active carbon filter links to each other with the entrance point of security personnel's filters (5), the port of export of security personnel's filter links to each other by the entrance point of pump with modification reverse osmosis membrane filtration device (6), the concentrated solution outlet end of modification reverse osmosis membrane filtration device links to each other with concentrated flow container (8), concentrating the flow container port of export links to each other with concentrate delivery pump (9), the port of export of concentrate delivery pump links to each other with heat exchanger (10), the port of export of heat exchanger (10) links to each other with the entrance point of another heat exchanger (14), the port of export of heat exchanger (14) links to each other with the upper end of saltpetre sinking device (11), the upper end of saltpetre sinking device also links to each other with clear liquid jar (12), the outlet of clear liquid jar links to each other with clear liquid delivery pump (13), the port of export that cleans delivery pump links to each other with heat exchanger (10), and the bottom of saltpetre sinking device links to each other with centrifuge (15).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620088240 CN200945417Y (en) | 2006-08-21 | 2006-08-21 | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620088240 CN200945417Y (en) | 2006-08-21 | 2006-08-21 | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN200945417Y true CN200945417Y (en) | 2007-09-12 |
Family
ID=38732478
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200620088240 Expired - Lifetime CN200945417Y (en) | 2006-08-21 | 2006-08-21 | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN200945417Y (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671832B (en) * | 2009-10-14 | 2011-08-03 | 山东东岳氟硅材料有限公司 | Method for improving brine processing capability of brine preprocessor |
| CN102649594A (en) * | 2012-02-28 | 2012-08-29 | 东营华泰化工集团有限公司 | Nitrate removal technology by membrane method |
| CN102849756A (en) * | 2012-09-17 | 2013-01-02 | 广州新普利节能环保科技有限公司 | Device and method for nitre extraction of sodium sulfate type bittern |
-
2006
- 2006-08-21 CN CN 200620088240 patent/CN200945417Y/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671832B (en) * | 2009-10-14 | 2011-08-03 | 山东东岳氟硅材料有限公司 | Method for improving brine processing capability of brine preprocessor |
| CN102649594A (en) * | 2012-02-28 | 2012-08-29 | 东营华泰化工集团有限公司 | Nitrate removal technology by membrane method |
| CN102849756A (en) * | 2012-09-17 | 2013-01-02 | 广州新普利节能环保科技有限公司 | Device and method for nitre extraction of sodium sulfate type bittern |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106587446B (en) | A kind of power plant desulfurization wastewater dechloratation method | |
| CN205419857U (en) | Cloudy cation exchange system | |
| CN106492639B (en) | To adsorb the method for mentioning the obtained eluent of lithium and preparing lithium chloride concentrate as raw material | |
| CN104761076A (en) | Reverse osmosis water purification machine-intelligent pure water forward/reverse-alternate flushing water-saving system and method | |
| CN102923736A (en) | Processing method for refining industrial brine | |
| CN207331079U (en) | A kind of device for production water supply javelle water | |
| CN104628186A (en) | Method for treating sodium ion exchanger regenerated waste liquor in wastewater zero emission process and recycling system | |
| CN104624250A (en) | Chelate resin tower regeneration method | |
| CN200945417Y (en) | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution | |
| CN102874945A (en) | Pure water purification device | |
| CN215161499U (en) | Reverse osmosis pure water treatment water saving fixtures | |
| CN102092880B (en) | Process for freezing and denitriding primary brine with membrane method in polyvinyl chloride production | |
| CN213141592U (en) | High rate of recovery reuse of reclaimed water advanced treatment system | |
| CN202881038U (en) | Electroplating waste water separation and recycling treatment apparatus | |
| CN1184005A (en) | Electrical ion exchange resin regenerating method and equipment | |
| CN101787541B (en) | Method for removing nitrates through CIM membrane method | |
| CN106746046A (en) | Process unit and method that ionic membrane realizes desulfurization waste liquor zero-emission are driven based on electricity | |
| CN203507825U (en) | New recovery system for recovering acid and alkali from viscose sodium sulfate waste liquid by bipolar membrane electrodialysis method | |
| CN207685025U (en) | Water warfare reclaiming system in a kind of pharmaceutical factory | |
| CN204607728U (en) | A kind of reverse osmosis water purifier and intelligent pure water back flushing water-saving system | |
| CN204569588U (en) | A kind of reverse osmosis water purifier and intelligent pure water just rinse water-saving system | |
| CN203922755U (en) | Brine desulfuration system | |
| CN203393287U (en) | System for recovering acid and alkali from viscose sodium sulfate waste liquor by bipolar membrane electrodialysis method | |
| CN202808515U (en) | Device for producing purified water by utilizing phosphatizing waste water | |
| CN210736911U (en) | Prevent blockking up electrolysis trough brine circulating system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20070912 |
|
| EXPY | Termination of patent right or utility model |