CN104843742B - A kind of brine system silicon removing method - Google Patents
A kind of brine system silicon removing method Download PDFInfo
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- CN104843742B CN104843742B CN201510164539.5A CN201510164539A CN104843742B CN 104843742 B CN104843742 B CN 104843742B CN 201510164539 A CN201510164539 A CN 201510164539A CN 104843742 B CN104843742 B CN 104843742B
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- salt
- preprocessor
- silicon
- ferric chloride
- sea salt
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Abstract
The present invention relates to a kind of brine system silicon removing method, including committed step：It is mixed in proportion interpolation sea salt, the key component of sea salt, and add appropriate ferric chloride.And increase lime water or soda regulating system at reaction tank before salt dissolving, and increase sodium hydroxide regulating system and preprocessor outlet pH detecting system in rear reaction tank.By process adjustments, reacted and deposited absorption silicon, last blowdown deposit in salt water preprocessor, so that dioxide-containing silica in primary brine system is reduced rapidly, reach below 5mg/L, meet film caustic soda process production requirement.
Description
Technical field
The present invention relates to saline removes silicon field and in particular to a kind of brine system silicon removing method.
Background technology
Saline is not only, except silicon, the technical barrier that chlor-alkali industry faces, and even more many chlor-alkali producers are urgently to be resolved hurrily at present
Problem, the applicant's chlor-alkali production brine system, analysis in the near future finds the exceeded always (salt of silicone content in brine system
Water SiO2Du Pont Analysis 12.8～20mg/l), subsequent subsidiary factory just actively implements test and seeks reduction silicon and silicon removing method.
Due to silicon excessive problem in first time experience saline, no ready-made Technical Solving and also no ripe in the industry
Technical scheme, but visit with the same industry exchange in find that this problem is widely present, and inquire into silicon occur exceeded the reason
When, find occur silicon exceeded the reason：1st, during ion film caustic soda produces, saline is to recycle, and silicon is long in brine system
Caused by phase accumulation, often can exceed 10mg/L；2nd, it has been mixed into portland cement due in crude salt：As Yan Ku ground, forklift shovel salt, change
Concrete grey is brought into when salt pond is damaged etc..3rd, the salt kind of a part of producer is occurred by originally all being used instead after rock salt using sea salt
's.
Find silicon exceeded the reason after, immediately discuss analysis taken out three sets of solutions：1) implement to arrange outside saline, can
See effect immediately.But this scheme not only can increase salt consumption but also environmental protection can't pass, so inadvisable；2) adopt in chlor-alkali industry
Add the silicon removing methods such as magnesium chloride, not only cost is too high, and effect does not reach yet；3) using the research of technique of low cost.Due to salt
In water system, silicon dioxide is enriched with continuous, is increased to 20mg/L after one month.Subsidiary factory is broken through in desilication technique method,
Discovery Calx can reduce silicon dioxide in former salt, and successfully uses in former halogen.Through trying out one month, two in saline
Silicon oxide can only drop and drop to 12mg/L from 20mg/L, again do not drop, and Calx is also not ideal except silicon effect, then stopped stone
Ash removes silicon, then carries out new method exploration.
Content of the invention
For above-mentioned technical problem, it is an object of the invention to provide a kind of brine system silicon removing method, particular technique side
Case is as follows：
A kind of brine system silicon removing method, further, is mixed in proportion interpolation sea salt, and adds appropriate tri-chlorination
Ferrum.
Further, the step being mixed in proportion interpolation sea salt is carried out in salt dissolving pond.
Further, salt dissolving pond is added sea salt daily and is added by the range of the 20%-30% of consumption per day, can quickly reduce salt
Silicone content in water.
Further, after silicone content is up to standard, sea salt by consumption per day 10%-20% about in the range of persistently add, can
Keep silicone content in brine system will not accumulate increase again.
Further, add the step of ferric chloride in water distribution bucket, preprocessor import, and/or, salt dissolving pump inlet is entered
OK.Optimum between 10～200ppm for the ferric chloride scope.
Further, ferric chloride pass through preprocessor import blender at adjust, addition according to preprocessor above
Water quality color and excessively film iron content judge to adjust.Ferric chloride addition is 0.01-0.2m3/h.
Further, before Hua Chi pond reaction tank add appropriate (soda, lime water and sodium hydroxide) one of which or
Two kinds.
Further, the key component of sea salt：
Sea salt
Brief description
Fig. 1 removes silicon supplementary material for sea salt of the present invention and uses and analytical data cartogram
Fig. 2 removes silicon equipment schematic diagram for saline of the present invention
Specific embodiment
Describe the present invention below according to accompanying drawing, it is that one of numerous embodiments of the present invention are preferably real
Apply example.
First, course control method for use:
1st, add appropriate ferric chloride in light salt brine water distribution bucket, ferric chloride scope is optimal between 10～200ppm
Value, pH is certain interval between 3-11.
2nd, brine temp is maintained at the optimum between 40～80 DEG C.
3rd, pressurize pump discharge, and/or preprocessor exit pH, can add alkali by 2# baffling groove and adjust, control pH respectively
For 9-14, and in 7-13 between optimum.
4th, front reaction tank adds sodium hydroxide, and early stage excess controlling value in 0.4-0.6g/l, can reduce and control by the later stage
Optimum between 0.1-0.5g/l.
5th, front reaction tank adds soda, and early stage excess controlling value in 0.35-0.55g/l, can reduce and control in 0.1- by the later stage
Optimum between 0.5g/l.
6th, preprocessor tri-chlorination iron can be by adjusting at preprocessor import blender, and addition is according to preprocessor
Top water quality color and excessively film iron content judge to adjust.Ferric chloride concentration is 1%-5%, and ferric chloride addition is 0.01-
0.2m3/h.
7th, increase during using dosage sea salt and patrol and examine dynamics (at least per hour once) it is ensured that pre- locate above preprocessor
Reason device obtains down blow in time, and once, after blowdown, mud is processed in time for every two hours blowdown, and the pH of sludge water ensures certain
In 7～13 certain interval.
8th, all film saline indexs of crossing all need to control in the range of technological procedure index request.
9th, electrowinning process can organize and implement resin tower regeneration in time according to primary brine calcium-magnesium content and tank voltage situation.
10th, because using a certain amount of sea salt, blowdown flow rate increases, brine section organizes filter press work.
11st, pressurize pump discharge pH probe tube, and with easily stifled after a certain amount of sea salt, DCS need to pay close attention to pH trend, patrol and examine and need to pay close attention to pH
Measurement bucket flooded conditions.
2nd, analysis monitoring point in brine system during except silicon：
1st, pressurization pump discharge pH, calcium and magnesium and silicone content.
2nd, salt dissolving pump discharge silicone content.
3rd, cross film ferric chloride, calcium and magnesium, cross alkali number and silicone content.
4th, preprocessor overfall calcium and magnesium.
After removing silicon using this method, can determine whether out that saline silicone content is in be decreased obviously trend through analytical data, in two weeks
In saline, silicon dioxide can drop to below 5mg/L (see dioxide-containing silica analytical data cartogram) from 20mg/L.
Above in conjunction with accompanying drawing, the present invention is exemplarily described it is clear that the present invention implements is not subject to aforesaid way
Restriction, as long as employing method of the present invention design and the various improvement that carry out of technical scheme, or not improved direct application
In other occasions, all within protection scope of the present invention.
Claims (2)
1. a kind of brine system silicon removing method is it is characterised in that comprise the steps：
（1）It is mixed in proportion interpolation sea salt, carries out in salt dissolving pond, the 20%-30% that consumption per day pressed by daily interpolation sea salt adds；
（2）Ferric chloride passes through to adjust at preprocessor import blender；
（3）Add appropriate ferric chloride, be added on water distribution bucket, preprocessor import and/or salt dissolving pump inlet and carry out, tri-chlorination
Ferrum addition is 0.01-0.2m3/h；
（4）After silicone content is up to standard, sea salt is persistently added by the 10%-20% of consumption per day.
2. brine system silicon removing method as claimed in claim 1 is it is characterised in that step（3）Described in ferric chloride concentration
For 1%-5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510164539.5A CN104843742B (en) | 2015-04-08 | 2015-04-08 | A kind of brine system silicon removing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510164539.5A CN104843742B (en) | 2015-04-08 | 2015-04-08 | A kind of brine system silicon removing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104843742A CN104843742A (en) | 2015-08-19 |
| CN104843742B true CN104843742B (en) | 2017-03-01 |
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| CN108996773B (en) * | 2018-06-27 | 2021-09-07 | 德州实华化工有限公司 | Production process for refining secondary brine by using well mineral salt instead of solarized sea salt |
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| CN101724756A (en) * | 2009-12-31 | 2010-06-09 | 攀枝花新钢钒股份有限公司 | Phosphorus and silicon removing method of vanadium-contained clinker leaching liquor |
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