CN104649494A - Method for treating silica sol wastewater and co-producing sodium salt - Google Patents
Method for treating silica sol wastewater and co-producing sodium salt Download PDFInfo
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- CN104649494A CN104649494A CN201510051038.6A CN201510051038A CN104649494A CN 104649494 A CN104649494 A CN 104649494A CN 201510051038 A CN201510051038 A CN 201510051038A CN 104649494 A CN104649494 A CN 104649494A
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Abstract
The invention discloses a method for treating the silica sol wastewater and co-producing a sodium salt. The method comprises the following steps: (1) adjusting the pH value of the silica sol wastewater to 2-5, and performing oxidation treatment by chlorine dioxide or ozone; (2) after adsorbing the oxidized waste water by an adsorber, adopting a reverse osmosis membrane or ion exchange resin to perform adsorption and concentration to obtain a strong liquid I and a thin liquid; (3) adjusting the pH value of the strong liquid I to more than 14, performing evaporation and concentration, and cooling and separating to obtain a sodium salt and a strong liquid II; (4) heating up the strong liquid II to 80-90 DEG C and adjusting the pH value to 8.5-9.5, and separating to obtain sodium silicate nanahydrate and a strong liquid III. An advanced oxidation technology and reverse osmosis membrane treatment are combined in the whole process, the processing effect is excellent, the COD removal rate of the wastewater is high; the COD of the effluent is less than 10 mg/L, and the effluent can be used as the industrial water; the high-purity sodium silicate and the sodium salt can be separated and recovered in the process, and the added value of the wastewater treatment can be increased.
Description
Technical field
The present invention relates to Treating Industrial Wastewater field, be specifically related to a kind of process of silicon sol waste water and the method for coproduction sodium salt.
Background technology
Water glass divides two kinds, sodium metasilicate Na
4siO
4with Starso Na
2siO
3.Sodium metasilicate is uncommon, and water glass is a kind of soluble silicate, is commonly called as water glass, and commodity are called sodium silicate.Water glass be colourless orthogonal bipyramid crystallization or white to canescence block or powder, can weathering.Water glass crystal loses 6 molecular crystal water 100 DEG C time.Soluble in water, solution alkaline is greater than soda ash.
Water glass is a kind of important Inorganic Chemicals, except being used as Binder Composition, or manufactures the important source material of the fine chemical products such as silica gel, molecular sieve, silicon sol, white carbon black, and its purposes is very extensive, important role in national economy.
At present, domestic conventional silicon sol preparation method mainly contains ion exchange method, elemental silicon hydrolysis method, electrolytic electro-dialysis method, sour neutralisation, peptisation, polymerization sol method etc.Wherein, elemental silicon hydrolysis method product foreign matter content is few, particle diameter, SiO
2concentration etc. are easy to control, the good uniformity of gained silicon sol, and stability is high, and quality is better.Thus, the elemental silicon hydrolysis method that adopts prepares silicon sol more at present.
The technique that elemental silicon hydrolysis method prepares silicon sol is: elemental silicon evaporates and obtains finished product after catalysis, heating, dissolving.Pure silicon powder and deionized water reaction generate silicon sol, catalyzer sodium hydroxide then changes into stablizer sodium oxide etc., can produce in preparation process containing water glass and sodium-chlor mixing salt waste water, this waste water in acidity, impurity is less.If but the unprocessed direct discharge of high-salt wastewater, industrial and agricultural production water will certainly be closed and produce harm greatly aqueous bio, Drinking Water.
At present, for the process of brine waste, mainly concentrate on following method: (1) is under salinity is less than 20g/L condition, the process of high density salt solution can pass through salinity domestication, but domestication salinity concentration must improve gradually, system being tamed stage by stage requires salinity levels, and unexpected hypersaline environment can cause the failure of domestication and the delay of startup; (2) dilution method, make salinity lower than malicious threshold value, biological treatment would not be suppressed, but this method waste water resource, be prohibited; (3) evaporation concentration method, but contain multiple salt due to most of waste water, the salt of concentrated gained, mostly containing impurity, difficultly to be recycled.
As the publication number Chinese patent literature that is CN 103880239A discloses a kind for the treatment of process of brine waste, delivered to by brine waste in equalizing tank, after thermal pretreatment, enter triple effect evaporation, the water after separation is again through anaerobic reaction, second pond process.Gained purity salt is unknown and not easy to be recycled.
Publication number is the treatment process that the Chinese patent literature of CN 101734820A discloses a kind of high slat-containing wastewater, it is for the waste water of high saliferous, low COD, it is carried out multiple-effect evaporation concentration after coagulating kinetics, nanofiltration process, and the solid substance that multiple-effect evaporation obtains carries out burning or landfill according to the cleanup standard of solid waste.Add the burden of fixed-end forces so undoubtedly, and the salt in waste water can not be recycled.
Publication number is that the Chinese patent literature of CN 1792832A discloses a kind of process of epoxy resin brine waste and the recovery of salt.This invention relate to the process of a kind of epoxy resin brine waste and reclaims the method for salt, it is characterized in that in brine waste, add benzene homologues and/or methyl iso-butyl ketone (MIBK) extraction agent, extracting and separating upper organic phase returns epoxy resin and produces, lower floor's waste water first adds acidic substance and is neutralized to pH=5-9, separate underlying waste, upper liquid through being separated, concentrated, crystallization, dry finished product salt.Pre-treatment obtains single product salt.It adopts extraction, and industrially equipment is complicated, high cost.
Summary of the invention
The invention discloses a kind of process of silicon sol waste water and the method for coproduction sodium salt, for containing high density sodium salt composite waste, while process waste water, the sodium salt of separating high-purity, the high purity water glass recoverable obtained, other sodium salts reach industrial salt standard.
The process of silicon sol waste water and a method for coproduction sodium salt, comprise the following steps:
(1) by the pH regulator of silicon sol waste water to 2-5, then adopt dioxide peroxide or ozone to carry out oxide treatment;
(2) waste water after oxidation, after adsorbent, adopts reverse osmosis membrane or the process of ion exchange resin Adsorption Concentration, obtains dope I and light liquid;
(3) by more than the pH regulator to 14 of dope I, through evaporation concentration, refrigerated separation, sodium salt and dope II is obtained;
(4) dope II is heated to 80-90 DEG C, and by its pH regulator to 8.5-9.5, is separated and obtains sodium silicate nanahydrate and dope III.
In the present invention, first the pH of waste water is adjusted to 2-5, then adopts dioxide peroxide or ozone oxidation, remove larger molecular organics in water, reduce former water COD and colourity; Afterwards through absorption, treatment solution COD can be down to below 20mg/L; Re-use reverse osmosis membrane or ion exchange resin removes other impurity such as organism wherein further, be separated and obtain the higher dope I of pure saliferous and light liquid, now, main containing sodium salts such as water glass in dope I, fresh water can be back in the production of silicon sol.Dope I is adjusted to strong basicity, carry out concentrated after to lower the temperature separations, obtain sodium salt and dope II, dope II is adjusted to weakly alkaline, separation obtains sodium silicate colloidal and dope III.
Described dope III can as silicon sol waste water recycling in step (1), circular treatment.
Wherein, in step (1), Chlorine Dioxide Oxidation and ozone oxidation can adopt single or two kinds of couplings according to the particular case of waste water quality and oxidation effectiveness.
Adopt in Chlorine Dioxide Oxidation or ozone oxidation when chroma in waste water is less than 10000 times or COD≤2000mg/L any one; Chroma in waste water adopts two-stage oxidation when being greater than 10000 times or COD >=2000mg/L.
As preferably, in step (1), by the pH regulator to 5 of silicon sol waste water.
As preferably, in step (1), adopt Chlorine Dioxide Oxidation, in maintenance silicon sol waste water, the concentration of dioxide peroxide is 500-1500mg/L.
Dioxide peroxide can use chlorine dioxide generator to prepare, and also can add dioxide peroxide medicament.
As preferably, in step (1), adopt ozone oxidation, after ozone oxidation terminates, in the quality of waste water, in waste water, add the H that massfraction is 30%
2o
2, add-on is the 0.1%-0.2% of wastewater quality after oxidation.
As preferably, in step (2), sorbent material is at least one in gac, diatomite, attapulgite, aluminum oxide, wilkinite, and the add-on of sorbent material is the 0.1%-0.5% of wastewater quality after oxidation.
Further preferably, in step (2), sorbent material is gac and attapulgite, and the mass ratio of gac and attapulgite is 1: 3-5.
As preferably, in step (2), ion exchange resin is sodium form or chlorine type ion exchange resin.
The light liquid of part of step (2) gained can reuse in process for production of silicasol, dope I enters lower step process.
After the process of step (1) and (2), impurity in brine waste is removed substantially, wastewater pH > 14 is regulated (to continue after pH=14 to add the aqueous sodium hydroxide solution that massfraction is 2%, the quality added is the 1-4% of wastewater quality), now do not have sol precipitation to separate out, by MVR or multiple-effect evaporation, lower the temperature after sodium salt is separated out centrifugal, obtain pure sodium salt and dope II, the pH of dope II is adjusted to 8.5-9.5, sodium silicate nanahydrate colloid is now had to separate out, centrifugally obtain pure sodium silicate colloidal, dope III gets back in step (1), circular treatment.
As preferably, in step (4), the pH of dope II is adjusted to 9.
As preferably, in step (4), regulate pH with dilute hydrochloric acid, dilute sulphuric acid or dust technology, the massfraction of diluted acid is 1%-5%; The speed of adding is 1-10mL/min, and stirring velocity is 30-60r/min.The kind of diluted acid is determined according to the kind of sodium salt in waste water.
In step (4), when the pH of dope II is less than 8.5, in the water glass obtained, chlorion, sulfate ion or nitrate ion exceed standard; When pH is excessive, occur without colloid.With in the process of acid for adjusting pH, have colloid and engender, cause soltion viscosity to strengthen.When acid adding speed is excessive, easily cause localized acidity excessive, produce silicic acid; When stirring velocity is too small, in colloid, easily carry impurity secretly.
The present invention has the following advantages: whole technique adopts high-level oxidation technology to combine with reverse osmosis membrane processing, and treatment effect is good, and waste water COD clearance is high, and water outlet COD < 10mg/L, can be used for process water; The highly purified water glass of separable recovery and sodium salt in treating processes, improve the value added of wastewater treatment.
Accompanying drawing explanation
Fig. 1 is the schema of the process of silicon sol waste water of the present invention and the method for coproduction sodium salt.
Embodiment
Embodiment 1
Certain silicon sol waste water, pH=0.8, original COD=300mg/L, containing water glass and sodium-chlor mixing salt, salts contg (massfraction) about 9%.
With massfraction be 1% NaOH solution the pH of waste water is adjusted to 5, now have no jelly precipitation occur.Dioxide peroxide is passed in waste water, and keep chlorine dioxide concentration in solution to be about 500mg/L, oxidizing reaction is after 2 hours, the mixed adsorbent mass ratio mixed preparing of 1: 4 (gac and the attapulgite with) is added in waste water, add that quality is wastewater quality 0.1% of mixed adsorbent, whip attachment 20min, filters the water glass and the sodium-chlor mixing salt solution that obtain clear, colorless, now records the COD=13mg/L of solution.
Use reverse osmosis membrane to process further mixing salt solution, obtain dope I and light liquid.
Wherein, light liquid reuse, dope I massfraction is NaOH solution adjustment pH > 14 (continue after pH=14 to add the aqueous sodium hydroxide solution that massfraction is 2%, the quality added is the 1-4% of wastewater quality) of 2%, enters two effect MVR vapo(u)rization systems.
Stop concentrated when having a large amount of sodium-chlor to separate out, centrifugation after being cooled to 40 DEG C, the sodium-chlor obtained and dope II.
Sodium-chlor quality meets HG3255-2001 industrial goods quality standard, recoverable.
Dope II is heated to 80 DEG C, and the dilute hydrochloric acid that functional quality mark is 5% regulates its pH to 9, stirring reaction, and the speed that adds of dilute hydrochloric acid is 5mL/min, and stirring velocity is 50r/min.
Now have a large amount of sodium silicate nanahydrate colloid to separate out, recentrifuge is separated, and obtains sodium silicate colloidal and dope III.
Sodium silicate colloidal meets the quality standard of GB/T 4209-2008 liquid-2, can do industrial chemicals, binding agent etc., and wherein the content of water-insoluble is 0.20% (massfraction), and the content of sodium oxide is 2.5% (massfraction).
Dope III is back to use in next batch step (1), circular treatment.
Comparative example 1
In method of wastewater treatment described in embodiment 1, other conditions are constant, and dope I directly carries out evaporation concentration, produces white precipitate in concentration process in waste water, and the sodium chloride salt purity obtained is less than 80%, do not meet HG3255-2001 industrial goods quality standard.Known after testing: the white precipitate produced in concentration process is silicic acid.
Comparative example 2
In method of wastewater treatment described in embodiment 1, other conditions are constant, by the pH regulator to 8 of dope II, separate out all the time in stirring reaction process without colloid.
Comparative example 3
In method of wastewater treatment described in embodiment 1, other conditions are constant, dope I has lacked cooling step, the dope II that after dope I evaporation concentration, filtered while hot obtains after being separated regulates pH and heated and stirred is separated, containing chlorion in the sodium silicate colloidal obtained, sodium silicate colloidal meets the standard of GB/T 4209-2008 liquid-4, but in sodium silicate colloidal, the content of sodium oxide is 11.8%.
Comparative example 4
In method of wastewater treatment described in embodiment 1, other conditions are constant, and dope II does not heat, directly stirring and segregation after adjustment pH=9.Find to regulate in the process of pH and salt out, containing chlorion in the sodium silicate colloidal obtained, sodium silicate colloidal does not meet GB/T 4209-2008 standard, and in colloid, the content of sodium oxide is 15.5%.
Embodiment 2
Certain silicon sol waste water, pH=1, original COD=460mg/L, containing water glass and sodium sulfate mixing salt, salts contg is 12.5%.
By waste water massfraction be 1% NaOH solution regulate its pH=5.In solution, pass into ozone oxidation { flow of ozone is 2.5g/ (Lh) } after 1 hour, add the H that massfraction is 30%
2o
2, add H
2o
2quality be 0.1% of wastewater quality, stir.
Solution clear after process.
In waste water, add the mixed adsorbent mass ratio mixed preparing of 1: 5 (gac and the attapulgite with) again, add that quality is wastewater quality 0.5% of mixed adsorbent, filters.
Filter to obtain colourless saline solns, its COD=10mg/L.
Reverse osmosis membrane is used to process further the mixing salt solution after filtering.
Remove organism wherein, wherein fresh water part reuse.
The dense water massfraction that saliferous is higher is the NaOH solution adjustment pH > 14 of 2%, enters multi-effect evaporation system.
First separate out a large amount of sodium sulfate, centrifugation after being cooled to 25 DEG C, obtain sodium sulfate and dope II.Sodium sulfate quality meets GB/T6009-2003 quality standard.
Dope II is heated to 90 DEG C, and the dilute sulphuric acid that functional quality concentration is 2% regulates its pH to 9.5, stirring reaction, and the speed that adds of dilute sulphuric acid is 5mL/min, and stirring velocity is 50r/min.
Now there is a large amount of sodium silicate nanahydrate to separate out, be again separated, gained sodium silicate colloidal and dope III.
Sodium silicate colloidal meets the standard of GB/T 4209-2008 liquid-2, and dope III is back to use in next batch step (1), circular treatment.
Comparative example 5
In method of wastewater treatment described in embodiment 2, other conditions are constant, remove reverse osmosis step, direct evaporation concentration, be separated the micro-Huang of sodium sulfate salt obtained, the sodium silicate colloidal obtained has variegated, do not meet GB/T 4209-2008 standard, but in sodium silicate colloidal, the content of water-insoluble is 2.01%.
Embodiment 3
Certain silicon sol waste water, in acid, COD=600mg/L, containing water glass and sodium-chlor mixing salt, salts contg is about about 8%, and wherein sodium chloride content is about 3%.
Adjust wastewater pH=5, do not have sol precipitation to separate out, in solution, add gac, add that quality is wastewater quality 0.1% of gac.
Logical ozone oxidation { flow of ozone is 2g/ (Lh) } in solution again, ozone oxidation, after 2 hours, adds the H that massfraction is 30%
2o
2, add H
2o
2quality be 0.2% of wastewater quality, stir.
Obtain colourless solution, record the COD=20mg/L of now waste water.
Waste water after oxidation again through the absorption of sodium form ion exchange resin (crossing 180 times that post wastewater volume is resin volume), obtain totally containing mixed salt solution.
Regulate containing the pH > 14 of mixed salt solution, enter multi-effect evaporation system, after having a large amount of sodium-chlor to separate out, be cooled to 50 DEG C, centrifugal, obtain sodium-chlor and dope II.
Sodium-chlor quality meets HG3255-2001 industrial goods quality standard.
Thicken the pH=8.8 of liquid II with the dilute hydrochloric acid that massfraction is 3%, the speed that adds of dilute hydrochloric acid is 8mL/min.
Now there is sodium silicate colloidal to separate out, recentrifuge, reclaim water glass and dope III.
Sodium silicate colloidal meets the standard of GB/T 4209-2008 liquid-2.
Dope III is back to use in next batch step (1), circular treatment, and phlegma can do industrial Water circulation or make recirculated water and use.
Comparative example 6
In method of wastewater treatment described in embodiment 3, other conditions are constant, and after wastewater pH being adjusted to 2, ozone oxidation { flow of ozone is 2g/ (Lh) } 2 hours, adds the H that massfraction is 30%
2o
2, add H
2o
2quality be 0.2% of wastewater quality, stir.
Obtain colourless treatment solution, record the COD=144mg/L of waste water.Waste water COD=55mg/L after plastic resin treatment, finally obtains qualified salt and water glass.But when to cross post wastewater volume be 100 times, resin reaches capacity.
Claims (10)
1. the process of silicon sol waste water and a method for coproduction sodium salt, is characterized in that, comprise the following steps:
(1) by the pH regulator of silicon sol waste water to 2-5, then adopt dioxide peroxide or ozone to carry out oxide treatment;
(2) waste water after oxidation, after adsorbent, adopts reverse osmosis membrane or the process of ion exchange resin Adsorption Concentration, obtains dope I and light liquid;
(3) by more than the pH regulator to 14 of dope I, through evaporation concentration, refrigerated separation, sodium salt and dope II is obtained;
(4) dope II is heated to 80-90 DEG C, and by its pH regulator to 8.5-9.5, is separated and obtains sodium silicate nanahydrate and dope III.
2. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, described dope III can as silicon sol waste water recycling in step (1), circular treatment.
3. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, in step (1), by the pH regulator to 5 of silicon sol waste water.
4. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, in step (4), the pH of dope II is adjusted to 9.
5. the process of silicon sol waste water according to claim 4 and the method for coproduction sodium salt, is characterized in that, in step (4), regulate pH with dilute hydrochloric acid, dilute sulphuric acid or dust technology, the massfraction of diluted acid is 1%-5%.
6. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, in step (1), adopt Chlorine Dioxide Oxidation, the concentration keeping dioxide peroxide in silicon sol waste water is 500-1500mg/L.
7. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, in step (1), adopts ozone oxidation, after ozone oxidation terminates, in the quality of waste water, add the H that massfraction is 30% in waste water
2o
2, add-on is the 0.1%-0.2% of wastewater quality after oxidation.
8. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, it is characterized in that, in step (2), sorbent material is at least one in gac, diatomite, attapulgite, aluminum oxide, wilkinite, and the add-on of sorbent material is the 0.1%-0.5% of wastewater quality after oxidation.
9. the process of silicon sol waste water according to claim 8 and the method for coproduction sodium salt, is characterized in that, in step (2), sorbent material is gac and attapulgite, and the mass ratio of gac and attapulgite is 1: 3-5.
10. the process of silicon sol waste water according to claim 1 and the method for coproduction sodium salt, is characterized in that, in step (2), ion exchange resin is sodium form or chlorine type ion exchange resin.
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| CN105540943A (en) * | 2015-10-30 | 2016-05-04 | 中国石油化工股份有限公司 | Silicon-containing wastewater treatment method, silicon-containing wastewater utilization system, molecular sieve preparation method and molecular sieve preparation system |
| CN106145423A (en) * | 2016-08-31 | 2016-11-23 | 江苏久吾高科技股份有限公司 | A kind of epoxychloropropane based on membrane separation technique produces the processing method and processing device of waste water |
| CN111333272A (en) * | 2020-03-18 | 2020-06-26 | 潍坊润谱化学有限公司 | Method for treating industrial wastewater generated in production of p-methylsulfonylbenzaldehyde |
| CN111762847A (en) * | 2019-04-02 | 2020-10-13 | 上海凯鑫分离技术股份有限公司 | Resourceful treatment process of industrial high-concentration brine |
| CN114380448A (en) * | 2022-01-26 | 2022-04-22 | 海宁天纵电子科技有限公司 | Micro-incineration-method-based harmless treatment method for residual liquor of narcotic drugs |
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| CN111333272A (en) * | 2020-03-18 | 2020-06-26 | 潍坊润谱化学有限公司 | Method for treating industrial wastewater generated in production of p-methylsulfonylbenzaldehyde |
| CN111333272B (en) * | 2020-03-18 | 2022-04-22 | 潍坊润谱化学有限公司 | Method for treating industrial wastewater generated in production of p-methylsulfonylbenzaldehyde |
| CN114380448A (en) * | 2022-01-26 | 2022-04-22 | 海宁天纵电子科技有限公司 | Micro-incineration-method-based harmless treatment method for residual liquor of narcotic drugs |
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