CN101671832B - Method for improving brine processing capability of brine preprocessor - Google Patents
Method for improving brine processing capability of brine preprocessor Download PDFInfo
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- CN101671832B CN101671832B CN2009100192547A CN200910019254A CN101671832B CN 101671832 B CN101671832 B CN 101671832B CN 2009100192547 A CN2009100192547 A CN 2009100192547A CN 200910019254 A CN200910019254 A CN 200910019254A CN 101671832 B CN101671832 B CN 101671832B
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Abstract
The invention discloses a method for improving the brine processing capability of a brine preprocessor through a brine membrane filtering process, and refining agents A and B are added into saturated crude brine to enter a forward reaction barrel, and then the crude brine after reaction enters the preprocessor. After being preprocessed through the preprocessor under the condition of back mixing, the partial crude brine returns the forward reaction barrel through a reflux regulating valve and is then transported to the preprocessor by simultaneously improving the flow capability of a crude brine pump, a refining agent C is added into the preprocessed crude brine to enter a membrane filter after reaction, and refined brine is discharged through a clear solution cavity of the membrane filter and then enters a refined brine tank after an amount of sodium sulfite is added to remove free chlorine. The invention ensures the stable water outlet of one-time refined brine by improving the brine processing capability of the brine preprocessor under the condition of crude salt quality fluctuation, achieves the purpose of stabilizing the running of a caustic soda device, and is simple and feasible.
Description
Technical field:
The present invention relates to ion film caustic soda primary brine treatment process, the particularly raising of pretreater demagging ability has enlarged the buying scope of crude salt.
Background technology:
Producing primary brine technology at present popular and widely used at ion film caustic soda is the embrane method filtration process, it handles demagging effect and ability that the brinish key is pretreater, saturated crude brine after the change salt adds finishing agents such as clorox, sodium hydroxide in proportion respectively and advances preceding reactive tank stirring, and the reaction times was controlled at 30 minutes; When advancing pretreater, add the molysite pretreating agent in proportion, salt solution was controlled at 30 minutes through adding the yellow soda ash stirring reaction time after the pre-treatment.Molysite is the another kind of crucial medicament that guarantees pretreating effect, and the molysite that generally adds 15-45PPm according to the situation of crude salt can adsorb natural organic matter effectively, improves filtration capacity.Improve purification efficiency, protection is the step operation down.Pretreatment time is another important parameter, should be controlled at 30 minutes.If the brine treatment amount increases, will reduce reaction, pre-treatment equal time, cause reaction, pre-treatment is not thorough, influence refining effect, therefore must keep treatment capacity basicly stable, but under the excessive situation of salt quality instability especially Ca, Mg content overproof, keep original treatment capacity just can not satisfy the brinish demand, so will guarantee that qualified salt solution will reduce the primary brine aquifer yield.
Summary of the invention:
The object of the present invention is to provide a kind of method that improves pretreater demagging ability, under the unsettled situation of salt quality, keep the primary brine aquifer yield, satisfy the primary brine demand of soda equipment.
The technical scheme that the present invention takes is as follows:
The invention provides a kind of method that improves brine processing capability of brine preprocessor, comprise the following steps:
1) light salt brine that returns of electrolysis, steam condensate are pumped to salt dissolving tank salt after distributing trough mixes;
Add finishing agent A and finishing agent B when 2) the thick saturated brine that comes out of salt dissolving tank is flowed through the baffling groove; Be pumped in the pretreater after the reaction container reaction is finished before entering and remove salt slurry according to the stratified principle of the different insoluble substance of proportion;
3) go out thick saturated brine reaction container before pipeline refluxes back of 5%～40% of pretreater; 60～95% thick saturated brine flows into the afterreaction bucket and adds finishing agent C, after the reaction, enters the brine film strainer, utilizes the micropore interception capacity of polymeric material film pipe in the strainer, and the trickle magazine particle of removing in the salt solution becomes refined brine one time; Primary brine is stored in the refined brine storage tank after adding S-WAT and hydrochloric acid Ex-all free chlorine and regulating pH value.
After operation after a while, film filter should enter acid cleaning process, recovers the millipore filtration ability of film pipe.
Described acid cleaning process is: at first, the salt solution in the strainer is all put only, and opened stifle on the strainer tube sheet; About 15% the hydrochloric acid that will prepare is in advance then squeezed into strainer, makes it soak full strainer; Open strainer pressurized air valve, slight bubbling stirred 1 hour; At last acid solution is emitted.After cleaning end, strainer advances salt solution and restarts filtration procedure.
Preferably, finishing agent A is selected from soda ash, caustic soda, clorox;
Preferably, finishing agent B is selected from clorox, hydrochloric acid or sulfuric acid.
Preferably, finishing agent C is selected from soda ash, caustic soda or sulfuric acid.
On pretreater brine outlet pipeline, increase the crude brine pipeline of reaction container before going, according to Mg content in crude salt or the crude brine with variable valve control return brine flow the normal sendout of crude salt water pump 5%～40% after, corresponding increase crude brine pump outlet flow.
This moment, return flow and pretreater discharge sum were the crude brine pumping capacity, continued to keep the constant and magnesium≤20PP of pretreater outlet brine flow.Effectively reduce the processing load of pretreater, reduce the backwash frequency of film filter.
The invention has the beneficial effects as follows: existing installation does not need big improvement, do not increase more equipment, adjust quantity of reflux by crude brine Ca, Mg content after analysis crude salt or the reaction by return valve and make pretreater increase by 10%～30%, thereby increase come-up flow raising pretreater is handled the salt outlet capacity.In Mg2+, ability improves 10%～30%.
Thereby the brine flow that is transported to pretreater improves pretreater by brine flow by opening return valve and increasing the crude brine pumping capacity, and then improves pretreater and handle the salt outlet capacity.
Description of drawings:
Fig. 1 is the FB(flow block) of brine rectification process in the embodiment of the invention.
Embodiment:
Below with specific embodiment technical scheme of the present invention is described, but protection scope of the present invention is not limited thereto:
Embodiment 1
1) light salt brine that returns of electrolysis, steam condensate are pumped to salt dissolving tank salt after distributing trough mixes;
Add finishing agent A (caustic soda) and finishing agent B (clorox) when 2) the thick saturated brine that comes out of salt dissolving tank is flowed through the baffling groove; Enter preceding reaction container, preceding reaction container Mg content 250ppm is pumped in the pretreater after reaction is finished and removes salt slurry according to the stratified principle of the different insoluble substance of proportion;
3) after desilt is finished in pretreater, thick saturated brine reaction container before pipeline refluxes back of 10%; 90% thick saturated brine flows into the afterreaction bucket and adds finishing agent C (yellow soda ash), after the reaction, enter the brine film strainer, utilize the micropore interception capacity of polymeric material film pipe in the strainer, the trickle magazine particle of removing in the salt solution becomes refined brine one time, is stored in the refined brine storage tank.
After operation after a while, film filter should enter acid cleaning process, recovers the millipore filtration ability of film pipe.
Reaction container Mg content 250ppm before this moment primary brine workshop section, so the crude brine pumping capacity is improved 10%, pretreater return valve quantity of reflux on year-on-year basis is 10%, pretreater advances the film filter flow and keeps constant, analyze pretreater outlet Mg content 19ppm, film filter outlet salt solution Ca+Mg＜1ppm.
Embodiment 2
Other are with embodiment 1.Difference is:
Reaction container pond Mg content 380ppm before the primary brine workshop section, improve the crude brine pumping capacity and improve 30%, pretreater return valve quantity of reflux on year-on-year basis is 30%, pretreater advances the film filter flow and keeps constant, analyze pretreater outlet Mg content 18ppm, film filter outlet salt solution Ca+Mg＜1ppm.
Embodiment 3
Other are with embodiment 1.Difference is: finishing agent A is a soda ash, and finishing agent B is a sulfuric acid, and finishing agent C is a caustic soda.
Embodiment 4
Other are with embodiment 1.Difference is: finishing agent A is a clorox, and finishing agent B is a hydrochloric acid, and finishing agent C is a sulfuric acid.
Claims (2)
1. a method that improves brine processing capability of brine preprocessor comprises the following steps:
1) light salt brine that returns of electrolysis, steam condensate are pumped to salt dissolving tank salt after distributing trough mixes;
Add finishing agent A and finishing agent B when 2) the thick saturated brine that comes out of salt dissolving tank is flowed through the baffling groove; Be pumped in the pretreater after the reaction container reaction is finished before entering and remove salt slurry according to the stratified principle of the different insoluble substance of proportion;
3) go out thick saturated brine reaction container before pipeline refluxes back of 5%～40% of pretreater; 60～95% thick saturated brine flows into the afterreaction bucket and adds finishing agent C, after the reaction, enters the brine film strainer, utilizes the micropore interception capacity of polymeric material film pipe in the strainer, and the fine impurity particle of removing in the salt solution becomes refined brine one time; Be stored in the refined brine storage tank after one time refined brine adds S-WAT and hydrochloric acid Ex-all free chlorine and regulates the pH value;
Finishing agent A is selected from soda ash, caustic soda or clorox;
Finishing agent B is selected from clorox, hydrochloric acid or sulfuric acid;
Finishing agent C is selected from soda ash, caustic soda or sulfuric acid.
2. the method for raising brine processing capability of brine preprocessor as claimed in claim 1 is characterized in that, after operation after a while, film filter enters acid cleaning process, recovers the millipore filtration ability of film pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2009100192547A CN101671832B (en) | 2009-10-14 | 2009-10-14 | Method for improving brine processing capability of brine preprocessor |
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| CN2009100192547A CN101671832B (en) | 2009-10-14 | 2009-10-14 | Method for improving brine processing capability of brine preprocessor |
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| CN101671832A CN101671832A (en) | 2010-03-17 |
| CN101671832B true CN101671832B (en) | 2011-08-03 |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103449479A (en) * | 2013-09-12 | 2013-12-18 | 山东东岳氟硅材料有限公司 | Method for reducing content of calcium and magnesium ions in primary brine |
| CN104928716B (en) * | 2015-05-26 | 2017-05-10 | 南通星球石墨设备有限公司 | Light salt brine pretreatment device |
| CN108950590A (en) * | 2018-07-11 | 2018-12-07 | 青海盐湖工业股份有限公司 | A kind of system and method for primary brine quality in control chlor-alkali production |
| CN109133110A (en) * | 2018-08-06 | 2019-01-04 | 广西田东锦盛化工有限公司 | Primary brine preparation method |
| CN110775991B (en) * | 2019-12-04 | 2022-04-08 | 攀枝花钢企欣宇化工有限公司 | Primary brine refining reaction system and control process thereof |
| CN112363480A (en) * | 2020-09-10 | 2021-02-12 | 唐山三友化工股份有限公司 | Brine large-system optimization control system based on material balance |
| CN111847482A (en) * | 2020-09-11 | 2020-10-30 | 连云港碱业有限公司 | System and method for preparing crude brine by ammonia-soda process |
| CN113461032A (en) * | 2021-07-20 | 2021-10-01 | 四川永祥股份有限公司 | Potassium control process and refining system for brine in sodium hydroxide production |
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| CN1868878A (en) * | 2006-03-15 | 2006-11-29 | 南京九思高科技有限公司 | Method of refining salt by membrane filtration |
| CN200945417Y (en) * | 2006-08-21 | 2007-09-12 | 山东布莱恩化工技术有限公司 | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution |
| CN101041487A (en) * | 2007-03-20 | 2007-09-26 | 山东布莱恩化工技术有限公司 | Pretreatment method for sulfate radical removal from salt water by membrane process |
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| CN1868878A (en) * | 2006-03-15 | 2006-11-29 | 南京九思高科技有限公司 | Method of refining salt by membrane filtration |
| CN200945417Y (en) * | 2006-08-21 | 2007-09-12 | 山东布莱恩化工技术有限公司 | Modified reverse osmosis membrane device used for removing sulfate radical from dilute salt solution |
| CN101041487A (en) * | 2007-03-20 | 2007-09-26 | 山东布莱恩化工技术有限公司 | Pretreatment method for sulfate radical removal from salt water by membrane process |
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| CN101671832A (en) | 2010-03-17 |
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