CN109319910B - Composite medicament for removing silicon by mine water evaporation crystallization water inflow and application thereof - Google Patents
Composite medicament for removing silicon by mine water evaporation crystallization water inflow and application thereof Download PDFInfo
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- CN109319910B CN109319910B CN201811306255.5A CN201811306255A CN109319910B CN 109319910 B CN109319910 B CN 109319910B CN 201811306255 A CN201811306255 A CN 201811306255A CN 109319910 B CN109319910 B CN 109319910B
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- C02F1/00—Treatment of water, waste water, or sewage
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Abstract
The embodiment of the invention provides a composite medicament for removing silicon from mine water evaporative crystallization influent water (TDS is more than 11 ten thousand ppm) and application thereof, wherein the composite medicament comprises sodium metaaluminate and soluble magnesium salt; the soluble magnesium salt is selected from magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate; the mass ratio of the sodium metaaluminate to the soluble magnesium salt is 1 (1.66-4). By adopting the composite reagent for mine water evaporative crystallization water inlet desilicification and the desilicification method applying the composite reagent provided by the embodiment of the invention, the removal rate of silicon in concentrated mine water can be effectively improved while the dosage of a magnesium agent is reduced, the removal rate can reach over 90 percent, the purpose of deep desilicification is achieved, and the removal rate of the traditional desilicification method under the condition of high salt is about 50 to 70 percent.
Description
Technical Field
The invention relates to the technical field of desiliconization of high-salt mine water, in particular to a desiliconization composite agent for mine water evaporative crystallization inlet water and application thereof.
Background
The mine water refers to all water permeating into an underground mining space in the coal mining process, and sometimes contains a small amount of permeated surface water; the mine water with high mineralization degree contains a large amount of inorganic salt, and the mineral water enters evaporation crystallization equipment after being concentrated by a membrane technology to be subjected to resource utilization mainly by salt preparation. However, the concentrated mine water contains high-concentration impurity silicon, which can seriously affect the quality and purity of salt products; meanwhile, the evaporation crystallization equipment is scaled, polluted and blocked due to too high silicon content and needs to be cleaned frequently; frequent cleaning seriously affects the service life of evaporative crystallization equipment, and the evaporative crystallization equipment is frequently shut down, so that the operation is complicated, the treatment capacity is reduced, and zero emission cannot be realized, therefore, the silicon content (SiO) of the evaporative crystallization inlet water of mine water is often required2Calculated) is not higher than 40 mg/L.
In the prior art, the desiliconization of mine water is usually carried out by adopting excessive magnesium or aluminum agent before membrane concentration; although the content of silicon is low before concentration, after concentration, the silicon in water is also concentrated to cause the concentration to rise again; generally, after concentration, the content of silicon in mine water is still about 200mg/L, and the water inlet requirement of a subsequent evaporative crystallization device cannot be met.
For the concentrated mine water, the salt content (TDS) can reach more than 11 ten thousand ppm generally, if the traditional magnesium agent is still used for removing silicon, even if the magnesium agent is excessively added, the removal rate of silicon can only reach about 50-70%, and the excessive magnesium ions can cause the scale formation of evaporation crystallization equipment, so the water inlet requirement of the evaporation crystallization equipment can not be met.
Furthermore, common silicon scavengers are aluminum salts, such as sodium metaaluminate, which on the one hand can form insoluble aluminum silicate compounds with silicic acid; on the other hand, sodium metaaluminate is dissolved in water to form aluminum hydroxide colloid which can absorb active silicon in water. However, the floc generated by the desiliconization reaction of aluminum salt has poor sedimentation performance, and the sludge-water separation of suspended matters in water cannot be completed by a precipitation process due to the high-salt environment of the concentrated mine water, so that the effective desiliconization cannot be realized.
Therefore, no effective silicon removal method exists for the concentrated mine water (namely the mine water evaporative crystallization inlet water) which enters the evaporative crystallization equipment.
Disclosure of Invention
The embodiment of the invention aims to provide a silicon removal composite agent for mine water evaporative crystallization influent water and application thereof, so as to realize effective silicon removal of the mine water evaporative crystallization influent water. The specific technical scheme is as follows:
the invention provides a composite medicament for removing silicon by mine water evaporation crystallization water inflow, which comprises sodium metaaluminate and soluble magnesium salt; the soluble magnesium salt is selected from magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate; the mass ratio of the sodium metaaluminate to the soluble magnesium salt is 1 (1.66-4).
The second aspect of the invention provides a method for removing silicon in mine water evaporative crystallization water by using the composite medicament of the first aspect of the invention, which comprises the following steps:
(1) preparing 420-1755g/L composite medicament stock solution;
(2) adjusting the pH value of the inlet water of evaporation crystallization of mine water to 8-10;
(3) adding the composite medicament stock solution into the mine water after the pH is adjusted for evaporation crystallization, and stirring for 50-70 minutes; the adding volume of the compound medicament storage solution is 1/(1000) -1500 of the water inlet volume of the evaporation crystallization of the mine water after the pH value is adjusted;
(4) adding a polyacrylamide flocculant into the stirred mine water evaporative crystallization inlet water according to the adding amount of 1-2mg/L, and standing and precipitating after stirring;
(5) and obtaining supernatant, namely the evaporated and crystallized water for desiliconizing the mine water.
In certain embodiments of the second aspect of the present invention, sodium hydroxide or calcium hydroxide is used in step (2) to adjust pH of the mine water evaporative crystallization feed water.
In some embodiments of the second aspect of the present invention, the stirring time is 5 to 15 minutes after the polyacrylamide is added in step (4).
In some embodiments of the second aspect of the present invention, in step (4), the polyaluminum chloride is added to the mine water evaporative crystallization feed water after standing and precipitating, and the mixture is stirred and then allowed to stand and precipitate again.
In some embodiments of the second aspect of the present invention, the polyaluminum chloride is added in an amount of 20 to 30mg/L and the stirring time is 10 minutes.
The silicon removal composite agent for the mine water evaporative crystallization influent and the silicon removal method using the same provided by the embodiment of the invention can effectively remove silicon in the mine water evaporative crystallization influent, and the silicon removal rate can reach more than 90%; after silicon is removed, the silicon content in the water is not higher than 40 mg/L. Furthermore, the composite medicament and the method for removing silicon have the residual quantity of magnesium ions less than or equal to 10ppm after silicon removal, so that equipment scaling and fouling caused by the magnesium ions can be ignored.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a mine water evaporation crystallization water-feeding silicon removal reactor.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a composite medicament for removing silicon by mine water evaporation crystallization water inflow, which comprises sodium metaaluminate and soluble magnesium salt; the soluble magnesium salt is selected from magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate; the mass ratio of the sodium metaaluminate to the soluble magnesium salt is 1 (1.66-4).
Sodium metaaluminate, as well as soluble magnesium salts such as magnesium chloride hexahydrate, magnesium sulfate, magnesium nitrate hexahydrate, and the like, used in the present invention are commercially available.
The magnesium salt desilicification is the most commonly used desilicification method in the water treatment industry at present, however, the inventor discovers that for mine water evaporation crystallization inlet water, because the salt concentration is too high, the TDS value (reflecting the content of dissolved impurities in the water, and mainly being sodium chloride for the mine water evaporation crystallization inlet water) can reach more than 110000mg/L through pilot test and demonstration engineering field research; meanwhile, in order to avoid the structure of an evaporative crystallization device, the silicon content is required to be low, and the calcium and magnesium hardness content in inlet water is also required to be low; thus, the conventional method for removing silicon from magnesium salts is not applicable; taking the example of treating mine water evaporative crystallization feed water with magnesium chloride hexahydrate, when the adding amount reaches 1300mg/L, the silicon content in the mine water evaporative crystallization feed water is reduced from 190mg/L to 60-95mg/L (SiO is used2Calculated), the removal rate is only about 50-70%; the adding amount of magnesium chloride hexahydrate is increased, and the silicon content in the mine water evaporated and crystallized inlet water is not obviously reduced. Therefore, the traditional method for removing silicon from magnesium salt cannot meet the requirement that the silicon content of the inlet water of an evaporation crystallization device is less than 40mg/L for the evaporation crystallization inlet water of high-salt mine water. In the present invention, the "silicon content" is SiO unless otherwise specified2And (6) counting.
In addition, when sodium metaaluminate is used alone as a silicon removing agent, even under the action of a flocculating agent, the formed insoluble silicon compound has poor sedimentation performance, and the formed flocculate is difficult to separate from the water body.
The inventor unexpectedly discovers in the research that when sodium metaaluminate and soluble magnesium salt, especially magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate are mixed according to the proportion of the invention to prepare the compound medicament, the compound medicament is hydrolyzed in water to form colloid particles of aluminum hydroxide and magnesium hydroxide, and the colloid particles react with soluble silicon compounds in water to generate insoluble silicon compounds;under the action of anionic polyacrylamide, the generated insoluble silicon compound particles are gradually enlarged through flocculation, and are easy to settle. By adopting the method, the content of Silicon (SiO) in the mine water evaporative crystallization inlet water can be reduced2Calculated) is reduced to below 20mg/L from about 200mg/L, the silicon removal rate can reach about 90 percent, and the requirement that the silicon content of inlet water of an evaporative crystallization device is less than 40mg/L can be met; after the composite medicament is used for removing silicon, the residual quantity of magnesium ions is less than or equal to 10 ppm.
The second aspect of the invention provides a method for removing silicon in mine water evaporative crystallization water by using the composite medicament of the first aspect of the invention, which comprises the following steps:
(1) preparing 420-1755g/L composite medicament stock solution;
(2) adjusting the pH value of the inlet water of evaporation crystallization of mine water to 8-10;
(3) adding the compound medicament stock solution into the evaporated and crystallized inlet water of the mine water after the pH value is adjusted, and stirring for 50-70 minutes; the adding volume of the compound medicament storage solution is 1/(1000) -1500 of the water inlet volume of the evaporation crystallization of the mine water after the pH value is adjusted;
(4) adding a polyacrylamide flocculant into the stirred mine water evaporative crystallization inlet water according to the adding amount of 1-2mg/L, and standing and precipitating after stirring;
(5) and obtaining supernatant, namely the evaporated and crystallized water for desiliconizing the mine water.
In some embodiments of the second aspect of the present invention, sodium hydroxide or calcium hydroxide may be used in step (2) to adjust the pH of the mine water evaporative crystallization feed water, which is a common technical means in the field, and the present invention is not limited herein.
The traditional method for removing silicon from magnesium salt is adopted, in order to provide dissociation conditions for magnesium hydroxide molecules, the pH is generally required to be controlled to be more than 12, so that a large amount of alkaline agent is required to be added to adjust the pH, and the production cost is high; the inventor unexpectedly discovers that when the composite medicament is used for treating the mine water evaporative crystallization influent water, the pH value of the mine water evaporative crystallization influent water is adjusted to 8-10, the effective silicon removal can be realized, the pH value is further increased, and the silicon removal effect is not obviously influenced, so that when the composite medicament is used for removing the silicon from the mine water evaporative crystallization influent water, the pH value of the mine water evaporative crystallization influent water is adjusted to 8-10 in consideration of the adding amount of the alkaline agent. In addition, in order to reduce the cost in industrial production, the pH value is usually adjusted by adopting calcium hydroxide, and the pH value of the existing method is higher, so the adding amount of the calcium hydroxide is inevitably larger, and the residual calcium ions in water can cause equipment scaling; the pH value of the invention is lower, so the use amount of calcium hydroxide can be reduced, and the content of calcium ions in water is further reduced.
In some embodiments of the second aspect of the present invention, in step (3), the ratio of the added volume of the composite medicament storage solution to the volume of the water to be treated is determined according to the silicon content in the water to be treated; illustratively, the higher the silicon content is, the larger the volume ratio of the adding amount of the composite medicament stock solution to the water inflow of evaporative crystallization of mine water is.
In some embodiments of the second aspect of the present invention, the stirring time is 5 to 15 minutes after the polyacrylamide is added in step (4).
The polyaluminium chloride is used as a coagulant, can promote the precipitation of flocculate generated after the polyacrylamide is added, and is beneficial to improving the sedimentation effect. Therefore, in some embodiments of the second aspect of the present invention, in step (4), the polyaluminum chloride may be added to the mine water evaporative crystallization feed water after standing for precipitation, and standing for precipitation again after stirring to improve the precipitation effect of flocs.
In some embodiments of the second aspect of the present invention, the polyaluminum chloride is added in an amount of 20 to 30mg/L and the stirring time is 10 minutes.
The unit of the adding amount of the polyacrylamide and the polyaluminium chloride is mg/L, which means that the milligrams of the polyacrylamide or the polyaluminium chloride are added into the mine water evaporative crystallization inlet water after the pH is adjusted by 1L of the mine water, and the polyacrylamide flocculant is added into the mine water evaporative crystallization inlet water according to the adding amount of 1-2mg/L in the step (4), namely, 1-2mg of the polyacrylamide is added into the mine water evaporative crystallization inlet water after 1L of the mine water evaporative crystallization inlet water is treated; in some embodiments of the second aspect of the invention, the adding amount of the polyaluminium chloride is 20-30mg/L, which means that the mass of the polyaluminium chloride which needs to be added is 20-30mg per 1L of mine water evaporative crystallization inlet water.
In some embodiments of the present invention, the silicon removal using the complex reagent is performed in a reactor as shown in fig. 1:
the reactor sequentially comprises a reaction tank I1, a reaction tank II 2, a reaction tank III 3 and a sedimentation tank 4 according to the water flow direction; the reaction tank I1 and the reaction tank II 2 are respectively provided with a blade rapid stirrer 5; a frame type slow stirrer 6 is arranged in the reaction tank III 3; be provided with pipe chute filler 7 in the sedimentation tank 4 (more be favorable to the suspended solid to precipitate), arrange mud simultaneously and adopt the multiple spot to arrange the mud mode (because production mud has certain viscidity, this setting can avoid dirty stifled).
Adding alkali liquor into the reaction tank I1, stirring, and adjusting the pH value of inlet water of evaporation crystallization of mine water to 8-10; the reaction time is 5 minutes;
in the reaction tank II 2, adding the composite medicament storage solution into the mine water evaporation crystallization inlet water according to the volume ratio of the storage solution to the treated water volume of 1/(1000-1500), and stirring for 50-70 minutes;
adding polyacrylamide into the reaction tank III 3, wherein the adding amount is 20-30mg/L, and stirring for 10 minutes;
in the sedimentation tank 4, suspended matters generated in a front reaction zone realize sludge-water separation under the dual actions of gravity and inclined tube filler collision;
in some embodiments of the present invention, the PAC reagent is determined to be needed to be added according to whether a large amount of alum flocs are generated in the sedimentation tank and whether the silicon content of the effluent reaches the standard. When the alum floc amount is small and the silicon content of the effluent exceeds the standard, PAC (polyaluminium chloride) needs to be added additionally to promote the formation of large-particle suspended matters. When the silicon content of the effluent meets the requirement, the addition can be omitted.
Example of using the composite medicament provided by the invention to remove silicon from mine water evaporative crystallization inlet water
The quality of the mine water evaporative crystallization inlet water adopted in the embodiment of the invention is as follows: the raw water is nanofiltration produced water, and after reverse osmosis and high-pressure reverse osmosis concentration, TDS (110000 mg/L) (mainly sodium chloride) is obtained; the COD value is 60 mg/L; total silicon content (in SiO)2Meter) 190mg/L, pH 5; the content of silicon in the effluent is required to be lower than 40mg/L, and in the following examples and comparative examples, the mine water evaporative crystallization influent is simply referred to as the water to be treated.
Example 1:
1. preparing a compound medicament stock solution: weighing 15g of sodium metaaluminate and 65g of magnesium chloride hexahydrate (the molar ratio is 1:1.78), dissolving in 100ml of water, and preparing 800g/L of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution;
2. pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 8, then adding 0.45mL of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution into the water to be treated, and reacting for 60min under the stirring of 200 r/min; adding anionic polyacrylamide according to the adding amount of 1mg/L for flocculation, slowly stirring for 5min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting that the silicon content of water is 16.24mg/L (using SiO2A meter); the residual amount of magnesium was 4.5 mg/L.
Example 2:
1. preparing a compound medicament stock solution: weighing 12g of sodium metaaluminate and 70g of magnesium sulfate (the molar ratio is 1:3.88), dissolving in 100ml of water, and preparing 820g/L of sodium metaaluminate-magnesium sulfate composite medicament stock solution;
2. pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH values to 9 respectively, then adding 0.25mL of sodium metaaluminate-magnesium sulfate composite medicament stock solution into the water to be treated, and reacting for 50min under the stirring of 200 r/min. Adding 1.5mg/L anionic polyacrylamide for flocculation, slowly stirring for 10min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting to obtain water with silicon content of 18.36mg/L (SiO2A meter); the residual amount of magnesium was 5.1 mg/L.
Example 3:
1. preparing a compound medicament stock solution: weighing 10g of sodium metaaluminate and 97g of magnesium nitrate hexahydrate (the molar ratio is 1:3.15), dissolving in 100ml of water, and preparing 1070g/L of sodium metaaluminate-magnesium nitrate hexahydrate composite medicament stock solution;
2. pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 10, and adding sodium hydroxide into the water to be treatedAdding 0.3mL of magnesium nitrate hexahydrate composite medicament stock solution, and reacting for 70min under stirring at 200 r/min; adding 2mg/L anionic polyacrylamide for flocculation, slowly stirring for 15min (stirring speed 100r/min), standing for 10min, adding 20mg/L polyaluminum chloride, slowly stirring for 10min (stirring speed 100r/min), standing to completely settle the generated floc, collecting supernatant, and detecting water silicon content to be 16.15mg/L (using SiO2A meter); the residual amount of magnesium was 5.05 mg/L.
Comparative example 1
Pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 12, then adding magnesium chloride hexahydrate into the water to be treated to enable the concentration of the magnesium chloride hexahydrate in the water to be treated to be 650mg/L, and reacting for 50min under the stirring of 200 r/min; adding 1.5mg/L anionic polyacrylamide for flocculation, slowly stirring for 10min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting water silicon content to 130.17mg/L (using SiO2Meter).
Comparative example 2
Pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 12, then adding magnesium chloride hexahydrate into the water to be treated to enable the concentration of the magnesium chloride hexahydrate in the water to be treated to be 970mg/L, and reacting for 70min under the stirring of 200 r/min; adding 2mg/L anionic polyacrylamide for flocculation, slowly stirring for 15min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting to obtain water with silicon content of 105.51mg/L (using SiO2Meter).
Comparative example 3
Pouring 300mL of water to be treated into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 12, then adding magnesium chloride hexahydrate into the water to be treated to enable the concentration of the magnesium chloride hexahydrate in the water to be treated to be 1200mg/L, and reacting for 70min under the stirring of 200 r/min; adding 2mg/L anionic polyacrylamide for flocculation, slowly stirring for 15min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting to obtain water with silicon content of 90.6mg/L (using SiO2Meter).
Comparative example 4:
1. preparing a compound medicament stock solution: weighing 13g of sodium metaaluminate and 160.5g of magnesium chloride hexahydrate, dissolving in 100ml of water, and preparing 1735g/L of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 8, then adding 0.3mL of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution into the wastewater, and reacting for 60min under the stirring of 200 r/min; adding anionic polyacrylamide according to the adding amount of 1mg/L for flocculation, slowly stirring for 5min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, taking supernatant to detect that the silicon content of water is 23.03mg/L (using SiO)2Meter).
Comparative example 5:
1. preparing a compound medicament stock solution: weighing 12g of sodium metaaluminate and 80g of magnesium sulfate, dissolving in 100ml of water, and preparing 920g/L sodium metaaluminate-magnesium sulfate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH values to 9 respectively, then adding 0.25mL of sodium metaaluminate-magnesium sulfate composite medicament stock solution into the wastewater, and reacting for 50min under the stirring of 200 r/min. Adding 1.5mg/L anionic polyacrylamide for flocculation, slowly stirring for 10min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting to obtain water with silicon content of 28.1mg/L (using SiO2Meter).
Comparative example 6:
1. preparing a compound medicament stock solution: weighing 10g of sodium metaaluminate and 140g of magnesium nitrate hexahydrate, dissolving in 100ml of water, and preparing 1500g/L of sodium metaaluminate-magnesium nitrate hexahydrate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 10, then adding 0.3mL of sodium metaaluminate-magnesium nitrate hexahydrate composite medicament stock solution into the wastewater, and reacting for 70min under the stirring of 200 r/min; adding 2mg/L anionic polyacrylamide for flocculation, slowly stirring for 15min (stirring speed 100r/min), standing for 10min, adding 20mg/L polyaluminum chloride, slowly stirring for 10min (stirring speed 100r/min), standing to completely settle the generated floc,taking supernatant to detect that the content of silicon in water is 22.5mg/L (by SiO)2Meter).
Comparative example 7:
1. preparing a compound medicament stock solution: weighing 18g of sodium metaaluminate and 65g of magnesium chloride hexahydrate, dissolving in 100ml of water, and preparing 830g/L of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 8, then adding 0.3mL of sodium metaaluminate-magnesium chloride hexahydrate composite medicament stock solution into the wastewater, and reacting for 60min under the stirring of 200 r/min; adding anionic polyacrylamide according to the adding amount of 1mg/L for flocculation, slowly stirring for 5min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting that the silicon content of water is 21.9mg/L (using SiO2Meter).
Comparative example 8:
1. preparing a compound medicament stock solution: weighing 15g of sodium metaaluminate and 30g of magnesium sulfate, dissolving in 100ml of water, and preparing 450g/L sodium metaaluminate-magnesium sulfate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH values to 9 respectively, then adding 0.25mL of sodium metaaluminate-magnesium sulfate composite medicament stock solution into the wastewater, and reacting for 50min under the stirring of 200 r/min. Adding 1.5mg/L anionic polyacrylamide for flocculation, slowly stirring for 10min (stirring speed 100r/min), standing for 10min to completely settle the generated floc, collecting supernatant, and detecting to obtain water with silicon content of 29.1mg/L (using SiO2Meter).
Comparative example 9:
1. preparing a compound medicament stock solution: weighing 12g of sodium metaaluminate and 54g of magnesium nitrate hexahydrate, dissolving in 100ml of water, and preparing 660g/L of sodium metaaluminate-magnesium nitrate hexahydrate composite medicament stock solution;
2. pouring 300mL of mine water concentrated high-salinity wastewater into a 500mL beaker, adding sodium hydroxide to adjust the pH value to 10, then adding 0.3mL of sodium metaaluminate-magnesium nitrate hexahydrate into the wastewater, and reacting for 70min under the stirring of 200 r/min; adding 2mg/L anionic polyacrylamide for flocculation, and slowly stirringStirring for 15min (stirring speed 100r/min), standing for 10min, adding 20mg/L polyaluminium chloride, slowly stirring for 10min (stirring speed 100r/min), standing to completely settle the generated floc, and collecting the supernatant to detect that the silicon content in water is 21.02mg/L (using SiO as a reference)2Meter).
In the embodiment 1-3, only partial values in the range of the compound medicament proportion are selected for illustration, and the method can realize that the silicon content is lower than 40mg/L when the silicon is removed in the medicament proportion range, and can realize the silicon removal rate of more than 90 percent for mine water evaporation crystallization water with the silicon content of about 200 mg/L. Comparative examples 4 to 9 show that the effect of 90% silicon removal rate cannot be achieved when the compounding ratio of the composite chemical is higher or lower than the compounding ratio range of the present invention, respectively.
All the embodiments in the present specification are described in a related manner, and the same and similar parts among the embodiments may be referred to each other, and each embodiment focuses on the differences from the other embodiments. In particular, for the system embodiment, since it is substantially similar to the method embodiment, the description is simple, and for the relevant points, reference may be made to the partial description of the method embodiment.
The above description is only for the preferred embodiment of the present invention, and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention shall fall within the protection scope of the present invention.
Claims (6)
1. The use of a composite medicament for removing silicon from mine water evaporative crystallization influent water is characterized in that the composite medicament comprises sodium metaaluminate and soluble magnesium salts; the soluble magnesium salt is selected from magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate; the mass ratio of the sodium metaaluminate to the soluble magnesium salt is 1 (1.66-4);
the TDS of the mine water evaporative crystallization inlet water is more than 110000 mg/L.
2. A method for removing silicon by using a composite medicament for mine water evaporative crystallization water inlet is characterized by comprising the following steps:
(1) preparing 420-1755g/L composite medicament stock solution; wherein the composite medicament comprises sodium metaaluminate and soluble magnesium salt; the soluble magnesium salt is selected from magnesium chloride hexahydrate, magnesium sulfate or magnesium nitrate hexahydrate; the mass ratio of the sodium metaaluminate to the soluble magnesium salt is 1 (1.66-4);
(2) adjusting the pH value of the inlet water of evaporation crystallization of mine water to 8-10;
(3) adding the compound medicament stock solution into the evaporated and crystallized inlet water of the mine water after the pH value is adjusted, and stirring for 50-70 minutes; the adding volume of the compound medicament storage solution is 1/(1000) -1500 of the water inlet volume of the evaporation crystallization of the mine water after the pH value is adjusted;
(4) adding a polyacrylamide flocculant into the stirred mine water evaporative crystallization inlet water according to the adding amount of 1-2mg/L, and standing and precipitating after stirring;
(5) and obtaining supernatant, namely the evaporated and crystallized water for desiliconizing the mine water.
3. The method of claim 2, wherein sodium hydroxide or calcium hydroxide is used in step (2) to adjust the pH of the feed water for evaporative crystallization of mine water.
4. The method of claim 2, wherein the stirring time is 5 to 15 minutes after the polyacrylamide is added in step (4).
5. The method as claimed in claim 2, wherein in the step (4), the polyaluminum chloride is added into the mine water evaporation crystallization inlet water after standing and precipitating, and the standing and precipitating are carried out again after stirring.
6. The method of claim 5, wherein the polyaluminum chloride is added in an amount of 20 to 30mg/L and the stirring time is 10 minutes.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5858245A (en) * | 1996-07-15 | 1999-01-12 | Union Oil Company Of California | Inhibition of silicate scale formation |
| CN102477493A (en) * | 2010-11-29 | 2012-05-30 | 攀钢集团钢铁钒钛股份有限公司 | Silicon-removing phosphorus-removing purifying method of sodium-modified vanadium-extraction leachate |
| CN102718296A (en) * | 2012-06-07 | 2012-10-10 | 江门市慧信净水材料有限公司 | Flocculant for low-residue drinking water treatment and preparation method thereof |
| CN104098164A (en) * | 2014-07-27 | 2014-10-15 | 西南石油大学 | Method for synchronously removing silicon and COD in refining waste water |
| CN105568731A (en) * | 2015-12-16 | 2016-05-11 | 陕西科技大学 | Non-timber black liquor self-causticizing synergy silica removal method |
| US20160176739A1 (en) * | 2014-05-26 | 2016-06-23 | Mitsubishi Heavy Industries, Ltd. | Water treatment device and water treatment method |
| CN207330611U (en) * | 2017-08-08 | 2018-05-08 | 博天环境工程（北京）有限公司 | A kind of coal chemical industry high slat-containing wastewater Zero-discharge treating process system |
| CN207525068U (en) * | 2017-09-26 | 2018-06-22 | 内蒙古久科康瑞环保科技有限公司 | The system of silica and hardness in a kind of removal industrial wastewater |
| CN108328780A (en) * | 2017-07-12 | 2018-07-27 | 江苏久吾高科技股份有限公司 | A kind of reuse method and device of wastewater from TiO2 factory |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5321860A (en) * | 1976-08-13 | 1978-02-28 | Mitsubishi Rayon Co Ltd | Method of decoloring colored waste liquid |
-
2018
- 2018-11-05 CN CN201811306255.5A patent/CN109319910B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5858245A (en) * | 1996-07-15 | 1999-01-12 | Union Oil Company Of California | Inhibition of silicate scale formation |
| CN102477493A (en) * | 2010-11-29 | 2012-05-30 | 攀钢集团钢铁钒钛股份有限公司 | Silicon-removing phosphorus-removing purifying method of sodium-modified vanadium-extraction leachate |
| CN102718296A (en) * | 2012-06-07 | 2012-10-10 | 江门市慧信净水材料有限公司 | Flocculant for low-residue drinking water treatment and preparation method thereof |
| US20160176739A1 (en) * | 2014-05-26 | 2016-06-23 | Mitsubishi Heavy Industries, Ltd. | Water treatment device and water treatment method |
| CN104098164A (en) * | 2014-07-27 | 2014-10-15 | 西南石油大学 | Method for synchronously removing silicon and COD in refining waste water |
| CN105568731A (en) * | 2015-12-16 | 2016-05-11 | 陕西科技大学 | Non-timber black liquor self-causticizing synergy silica removal method |
| CN108328780A (en) * | 2017-07-12 | 2018-07-27 | 江苏久吾高科技股份有限公司 | A kind of reuse method and device of wastewater from TiO2 factory |
| CN207330611U (en) * | 2017-08-08 | 2018-05-08 | 博天环境工程（北京）有限公司 | A kind of coal chemical industry high slat-containing wastewater Zero-discharge treating process system |
| CN207525068U (en) * | 2017-09-26 | 2018-06-22 | 内蒙古久科康瑞环保科技有限公司 | The system of silica and hardness in a kind of removal industrial wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 竹材硫酸盐法蒸煮中偏铝酸钠与硫酸镁的协同留硅机理;徐永建;《造纸科学与技术》;20151231;第34卷(第6期);第5-8、78页 * |
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