CN103539167A - Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process - Google Patents
Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process Download PDFInfo
- Publication number
- CN103539167A CN103539167A CN201210235093.7A CN201210235093A CN103539167A CN 103539167 A CN103539167 A CN 103539167A CN 201210235093 A CN201210235093 A CN 201210235093A CN 103539167 A CN103539167 A CN 103539167A
- Authority
- CN
- China
- Prior art keywords
- temperature
- purifying
- saltpetre
- speed
- waste
- 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.)
- Granted
Links
Images
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a method of continuously purifying potassium nitrate in batch in waste generated by a glass hardening process. The method mainly comprises the following steps: firstly, heating and melting the waste into waste liquor; then, purifying out potassium nitrate with different purities in batch from the waste liquor by utilizing multi-stage cooling with different rates, so that potassium nitrate can be recycled. The method has the advantages of being environment-friendly and capable of lowering cost.
Description
Technical field
The present invention relates to a kind of purification process of waste, refer to especially a kind of method of purifying saltpetre from glass sclerosis processing procedure waste that produce and that include saltpetre and SODIUMNITRATE effectively.
Background technology
General glass sclerosis processing procedure can be divided into physical hardening or chemicosolidifying, wherein, chemicosolidifying processing procedure is mainly that the water soda glass that will gain in strength immerses in saltpetre fused solution, by chemical ion permutoid reaction, the more untight sodium ion of glass structure will can be made in water soda glass, replace with the potassium ion in saltpetre fused solution, be about to sodium ion and replace with larger potassium ion, to promote the intensity of glass surface.
Due in the fused solution after chemical ion permutoid reaction for some time part saltpetre composition be exchanged for gradually SODIUMNITRATE, although and in industrial pure saltpetre fused solution, originally just contained micro-sodium ion, but when sodium nitrate concentration increases to a certain degree time, for example, sodium nitrate concentration in the fused solution reacting promotes after decades of times, the fused solution reacting just cannot carry out ion exchange reaction again, so that cannot really reach the object that promotes glass surface intensity.
Therefore, even if still contain saltpetre in the fused solution reacting, also unrenewable in chemicosolidifying processing procedure, hereat, conventionally for slight reduction cost, can the fused solution reacting be taken out by dilution mode, then rejoin pure saltpetre fused solution mixing use, and take out part, can only abandon as waste, very waste and not environmental protection, in addition, each dilution all needs to use a large amount of pure saltpetre fused solutions, causes manufacturing cost too high.
Summary of the invention
For the problems referred to above, main purpose of the present invention is to provide a kind of purification process, and it can be purified into most saltpetre in glass hardens the waste that processing procedure produces, and can obtain the saltpetre of different purity, makes saltpetre can be repeated recycling.
For achieving the above object, the method of continuous batch of purifying saltpetre in a kind of waste producing from glass sclerosis processing procedure provided by the present invention, described waste is solid-state and includes saltpetre and SODIUMNITRATE, the method of described purifying saltpetre includes the following step: (a) described waste is placed in to one first purifying groove, and described waste is heated to one can makes described castoff fusing become the melt temperature of a waste liquid, (b) with a First Speed, make described waste liquid be cooled to one first temperature from described melt temperature, and constant temperature is in described the first temperature, described the first temperature is enough to make described waste liquid to separate out potassium nitrate crystal and is attached to described the first purifying groove perisporium, (c) with a second speed that is slower than described First Speed, make described waste liquid from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre, (d) residue waste liquid is guided in one second purifying groove, (e) carry out following batch of step one of them: (e1) waste liquid in described the second purifying groove is heated to described melt temperature, and make described waste liquid be cooled to one first temperature from described melt temperature with a First Speed, and constant temperature is in described the first temperature, described the first temperature is enough to make described waste liquid to separate out potassium nitrate crystal and is attached to described the second purifying groove perisporium, and with a second speed that is slower than described First Speed, make described waste liquid from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre, (e2) potassium nitrate crystal that is attached to described the first purifying groove perisporium is heated to described melt temperature and becomes a fused solution, and carry out step (b) to (c), (e3) potassium nitrate crystal that is attached to described the first purifying groove perisporium is heated to described melt temperature and becomes a fused solution, described fused solution is guided in one the 3rd purifying groove, and make described fused solution be cooled to one first temperature from described melt temperature with a First Speed, and constant temperature is in described the first temperature, described the first temperature is enough to make described fused solution to separate out potassium nitrate crystal and is attached to described the 3rd purifying groove perisporium, and with a second speed that is slower than described First Speed, make described fused solution from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre, (f) potassium nitrate crystal of separating out is taken out.
In the technical scheme of the invention described above, step (c) afterwards with step (d) before, also include the third speed that is slower than described second speed with, make described waste liquid from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
Step (e1) also includes the third speed that is slower than described second speed with, make described waste liquid from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
Step (e2) and (e3) also include the third speed that is slower than described second speed with, make described fused solution from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
Described the 3rd temperature is in fact between 310 ℃ to 333 ℃.
By providing a thermal source in the bottom of described first, second and third purifying groove respectively, and the temperature of perisporium of controlling described first, second and third purifying groove is between 240 ℃ to 350 ℃, make waste liquid in described first and second purifying groove and the fused solution in described the 3rd purifying groove can keep constant temperature.
Described thermal source is one to be arranged at respectively the well heater of the bottom of described first, second and third purifying groove, and all wall temperatures of described first, second and third purifying groove are to control by a thermostatted that is coated on respectively described first, second and third purifying groove perisporium.
Described melt temperature is between 380 ℃ to 550 ℃.
Described the first temperature is between 340 ℃ to 350 ℃.
Described the second temperature is between 333 ℃ to 340 ℃.
Adopt technique scheme, the present invention is by above-mentioned " being cooled to the step of the 3rd temperature ", by making cooling rate more and more slower, saltpetre composition in waste liquid and fused solution can fully be separated out, and, because the present invention first becomes this waste heating and melting after waste liquid, again by stages with the temperature of different Speed Reduction waste liquids, and the step of collocation batch purifying, therefore not only can be purified into most saltpetre in waste liquid, can also obtain the saltpetre with different purity, make the saltpetre being purified into can be re-used in the processing procedure that glass hardens, therefore the advantage that there is environmental protection and can reduce costs.
Accompanying drawing explanation
Fig. 1 is the schema of the purification process of doing according to a preferred embodiment of the present invention;
Fig. 2 is a schematic diagram, the device that the purification process that demonstration is done according to this preferred embodiment of the present invention is used;
Fig. 3 is Fig. 2 roughly the same, shows that the another kind of the device that purification process of the present invention is used may form.
Embodiment
Now lift following examples and by reference to the accompanying drawings structure of the present invention and effect be elaborated.
Applicant is first in this explanation, and " approaching " word of addressing in specification sheets in the whole text refers to the meaning of " can higher than or lower than ".
First, as shown in Figure 1 and Figure 2, in a preferred embodiment provided by the present invention, in step S1, the processing procedure that first glass hardened produces includes saltpetre (potassium nitrate, KNO
3) and SODIUMNITRATE (sodium nitrate, NaNO
3) solid-state castoff insert in one first purifying groove 10, afterwards with a well heater 20 that is arranged at the first purifying groove 10 bottoms 23, be heated to the melt temperature of approximately 380 ℃ to 550 ℃, and at this temperature standing for some time, for example approximately 1 to 10 hours, make this waste be melt into a waste liquid W completely.In this example, by establishing a default temperature to a temperature regulator 30, an i.e. temperature between 380 ℃ to 550 ℃, make the temperature regulator 30 can be according to the temperature signal of temperature sensor 40 feedbacks, come control heater 20 and to be coated on the thermostatted 50 of the first purifying groove 10 perisporiums 21, and then make waste liquid W can be maintained at this default temperature.
About temperature regulator 30, temperature sensor 40 and thermostatted 50, in the present embodiment, temperature sensor 40 can use a high temperature modification thermometer, to measure the temperature of waste liquid W; Temperature regulator 30 is electrically connected to well heater 20, temperature sensor 40 and thermostatteds 50, makes temperature regulator 30 according to the temperature signal of the waste liquid W of temperature sensor 40 feedbacks, come control heater 20 and thermostatted 50 to heat up or cooling.So, the temperature of the waste liquid W in the first purifying groove 10 surpasses or during lower than default temperature, and temperature regulator 30 control heater 20 and thermostatted 50 coolings immediately or heat up, effectively to control the temperature of waste liquid W.
Due in the present embodiment, waste liquid W also includes except saltpetre (KNO
3) and SODIUMNITRATE (NaNO
3) other saline admixtures in addition, such as phosphoric acid salt (phosphate), vitriol (sulfate) or nitrite (nitrite), therefore the first purifying groove 10 preferably can be to make with the reactive stainless steel low and that have an anti-salt corrosion of potassium, sodium ion, to avoid the first purifying groove 10 to react with potassium, sodium ion, at the unnecessary reactant of the interior generation of the first purifying groove 10, and avoid the first purifying groove 10 to be at high temperature subject to aforementioned saline admixture corrode and damage.
Thereafter, the temperature of well heater 20 is maintained to aforementioned melt temperature (for example approximately 400 ℃), and make thermostatted 50 constant temperature in 240 ℃ to 350 ℃, make waste liquid W can be maintained at the temperature of approximately 310 ℃ to 350 ℃, then make waste liquid W carry out the stage cooling of step S2 to S3, namely, with more and more slower speed cooling, the saltpetre composition in waste liquid W can be separated out.For instance, first, in step S2, set one first temperature, be for example 350 ℃, namely a little more than the temperature of saltpetre freezing point temperature (being approximately 333 ℃), make afterwards waste liquid W with a First Speed, the speed of approximately 1.833 ℃/min in the present embodiment, start to be cooled to this first temperature, and constant temperature is in one period of scheduled time of this first temperature, in the present embodiment, this constant temperature time is (but being not limited to) approximately 1 hour, now, because the temperature of the waste liquid W of contiguous perisporium 21 can be a little less than the temperature of the waste liquid W of adjacent bottom 23, make the waste liquid W of contiguous perisporium 21 separate out gradually potassium nitrate crystal C and be attached to the internal surface of perisporium 21.Need special instruction, the visual actual demand of aforementioned constant temperature time and be 1 to 2 hour.
Afterwards, in step S3, set one second temperature, be for example 340 ℃, approach the temperature of saltpetre freezing point temperature (being approximately 333 ℃), afterwards with a second speed that is slower than this First Speed, the speed of approximately 0.014 ℃/min in the present embodiment, start to be cooled to this second temperature, and constant temperature is in the scheduled time of one section longer than above-mentioned constant temperature time of this second temperature, this constant temperature time is (but being not limited to) 2 hours in the present embodiment, and now, perisporium 21 can adhere to increasing potassium nitrate crystal C.Need special instruction, the visual actual demand of aforementioned constant temperature time and be 2 to 5 hours.
Therefore because this second temperature is zero pour (freezing point) temperature that approaches this saltpetre, longer constant temperature time can make to separate out in waste liquid W the potassium nitrate crystal C of volume more and be attached to the internal surface of the first purifying groove 10 perisporiums 21.
Come again, in step S4, remaining waste liquid W ' after carrying out for the first time purifying in the first purifying groove 10 is guided in one second purifying groove 10 '.For instance, as shown in Figure 2, remaining waste liquid W ' imports in the second purifying groove 10 ' by a coupling device 60.The design of the second purifying groove 10 ' is identical with the first purifying groove 10, and the second purifying groove 10 ' is equipped with well heater 20, temperature regulator 30, temperature sensor 40 and thermostatted 50 equally.And coupling device 60 includes such as general switch-valve or reverse checkvalve etc. of a valve 61(), a connecting pipe 63 and a heating unit 65.For withstand high temperatures, valve 61 can use such as metallic seal valve member, and aforementioned metal is stainless steel or copper; Heating unit 65, for controlling the temperature that flows into the waste liquid W ' in communicating pipe 63, makes waste liquid W ' be maintained at molten state.
After waste liquid W ' flows in the second purifying groove 10 ' by communicating pipe 63, then carry out step S51, waste liquid W ' is heated to aforementioned melt temperature, and carries out step S2 to S3, with further from waste liquid W ' by possible residual saltpetre purifying out.So, purification process of the present invention can be isolated most saltpetre in waste.
In the first purifying groove 10, remaining waste liquid W ' is imported into after the second purifying groove 10 ' completely, can carry out step S52, the potassium nitrate crystal that is attached to the first purifying groove 10 perisporiums 21 is heated to aforementioned melt temperature and becomes fused solution, and repeat step S2 to S3, with further purifying saltpetre in this fused solution, make purification process of the present invention can obtain the saltpetre with different purity.It is worth mentioning that, step S52, also can be as shown in Figure 3 except can carrying out in the first purifying groove 10 as previously mentioned, after becoming fused solution M, by coupling device 60, import one the 3rd purifying grooves 10 " in, and at the 3rd purifying groove 10 " in carry out abovementioned steps S2 to S3.Certainly, the 3rd purifying groove 10 " design also identical with the first purifying groove 10, i.e. the 3rd purifying groove 10 " well heater 20, temperature regulator 30, temperature sensor 40 and thermostatted 50 be equipped with equally.
Finally, respectively remaining waste liquid W ' after step S51 and S52 purifying is taken out, and collect potassium nitrate crystal C.Aforementioned taking-up waste liquid W ' and the method for collecting potassium nitrate crystal C, a kind of negative pressure insulation extraction tube device that can utilize previous the obtained TaiWan, China new patent of (but being not limited to) the present inventor to disclose for No. M426447, directly from first, second and third purifying groove 10,10 ', 10 " the interior saltpetre that extracts waste liquid W ' or molten state.
Certainly, during practical application, for the saltpetre remaining in waste liquid W ' is purified into as far as possible, and obtain the higher saltpetre of purity, above-mentioned batch (batch) purification step, step S51 and S52 can repeat depending on demand.
In addition, because this second temperature approaches zero pour (freezing point) temperature (being approximately 333 ℃) of this saltpetre, therefore, in waste liquid W ' in step S4, may remain the more saltpetre not being purified out, so, between the step S3 and S4 of purification process of the present invention, preferably also include the third speed that is slower than this second speed with, the speed of approximately 0.006 ℃/min in the present embodiment, make waste liquid W from this second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of the 3rd temperature, the 3rd temperature is about 310 ℃ in the present embodiment, namely higher than the temperature of SODIUMNITRATE freezing point temperature (being approximately 308 ℃), and its constant temperature time is (but being not limited to) 5 hours in the present embodiment, now, the speed of separating out of potassium nitrate crystal C can slow down gradually, to isolate further the saltpetre in waste liquid W and to avoid separating out the crystallization of SODIUMNITRATE simultaneously.Need special instruction, the 3rd temperature is in fact preferably between 310 ℃ to 333 ℃, and the visual actual demand of this constant temperature time is 5 to 15 hours.
In addition, during practical application, step S51 and step S52 can further include respectively foregoing with a third speed that is slower than this second speed equally, make waste liquid W ' and fused solution M from these the second temperature slow cooling to the three temperature, and constant temperature is in the step of the 3rd temperature, with further may undecomposed saltpetre purifying out.Aforementioned the 3rd temperature and this constant temperature time be identical with described in leading portion all.
Via the waste liquid W ' after the present embodiment purifying, utilize induction coupled plasma atomic emission spectrometry (Inductively Coupled Plasma Optical Emission Spectrometry, ICP-OES) detect the sodium ion amount in waste liquid W ', and, after calculating by following formula, therefore the sodium ion clearance of the purification process of this preferred embodiment of the present invention can reach 80%, provable the present invention purifying saltpetre from waste liquid effectively really.
[formula]
In addition, in the method for continuous batch of purifying saltpetre provided by the present invention, more can be at the first to the 3rd purifying groove 10,10 ' and 10 " in a liquidometer (not shown) is set respectively.This liquidometer can be arranged at the position of (but being not limited to) contiguous this purifying groove perisporium, to learn the general height of potassium nitrate crystal.In details of the words, this liquidometer is to utilize conducting circuit theory, just learns the height of potassium nitrate crystal by detecting conductance, for instance, while just having started to carry out purifying, liquidometer contact contains sodium, the isoionic waste liquid of potassium, now be conducting state, conductance is higher; When potassium nitrate crystal starts to separate out, the potassium nitrate crystal of separating out can be coated the detecting position of this liquidometer gradually, and now, owing to still having a small amount of waste liquid can infiltrate potassium nitrate crystal, although be therefore still conducting state, conductance reduces gradually; When crystallization envelopes the amount at detecting position of this liquidometer when more, waste liquid possibly cannot infiltrate potassium nitrate crystal again, so that conductance may be reduced to and approaches zero.So, by the conductance height recording, can learn the general height of potassium nitrate crystal.
In sum, because the present invention first becomes this waste heating and melting after waste liquid, again by stages with the temperature of different Speed Reduction waste liquids, and the step of collocation batch purifying, therefore not only can be purified into most saltpetre in waste liquid, can also obtain the saltpetre with different purity, make the saltpetre being purified into can be re-used in the processing procedure of glass sclerosis, so the advantage that there is environmental protection and can reduce costs.
Claims (10)
1. a method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure, described waste is solid-state and includes saltpetre and SODIUMNITRATE, the method for described purifying saltpetre includes the following step:
(a) described waste is placed in to one first purifying groove, and described waste is heated to one can makes described castoff fusing become the melt temperature of a waste liquid;
(b) with a First Speed, make described waste liquid be cooled to one first temperature from described melt temperature, and constant temperature is in described the first temperature, described the first temperature is enough to make described waste liquid to separate out potassium nitrate crystal and is attached to described the first purifying groove perisporium;
(c) with a second speed that is slower than described First Speed, make described waste liquid from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre;
(d) residue waste liquid is guided in one second purifying groove;
(e) carry out following batch of step one of them:
(e1) waste liquid in described the second purifying groove is heated to described melt temperature, and make described waste liquid be cooled to one first temperature from described melt temperature with a First Speed, and constant temperature is in described the first temperature, described the first temperature is enough to make described waste liquid to separate out potassium nitrate crystal and is attached to described the second purifying groove perisporium, and with a second speed that is slower than described First Speed, make described waste liquid from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre;
(e2) potassium nitrate crystal that is attached to described the first purifying groove perisporium is heated to described melt temperature and becomes a fused solution, and carry out step (b) to (c);
(e3) potassium nitrate crystal that is attached to described the first purifying groove perisporium is heated to described melt temperature and becomes a fused solution, described fused solution is guided in one the 3rd purifying groove, and make described fused solution be cooled to one first temperature from described melt temperature with a First Speed, and constant temperature is in described the first temperature, described the first temperature is enough to make described fused solution to separate out potassium nitrate crystal and is attached to described the 3rd purifying groove perisporium, and with a second speed that is slower than described First Speed, make described fused solution from described first temperature slow cooling to the second temperature, and constant temperature is in described the second temperature, described the second temperature approaches the freezing point temperature of described saltpetre,
(f) potassium nitrate crystal of separating out is taken out.
2. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, it is characterized in that: step (c) afterwards with step (d) before, also include the third speed that is slower than described second speed with, make described waste liquid from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
3. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, it is characterized in that: step (e1) also includes the third speed that is slower than described second speed with, make described waste liquid from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
4. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, it is characterized in that: step (e2) and (e3) also include the third speed that is slower than described second speed with, make described fused solution from described the second temperature slow cooling to the 3rd temperature, and constant temperature is in the step of described the 3rd temperature, described the 3rd temperature is higher than the freezing point temperature of described SODIUMNITRATE.
5. the method for continuous batch of purifying saltpetre in the glass sclerosis waste that processing procedure produced as described in any one in claim 2 to 4, is characterized in that: described the 3rd temperature is in fact between 310 ℃ to 333 ℃.
6. the method for continuous batch of purifying saltpetre in the glass sclerosis waste that processing procedure produced as described in any one in claim 2 to 4, it is characterized in that: by providing a thermal source in the bottom of described first, second and third purifying groove respectively, and the temperature of perisporium of controlling described first, second and third purifying groove is between 240 ℃ to 350 ℃, make waste liquid in described first and second purifying groove and the fused solution in described the 3rd purifying groove can keep constant temperature.
7. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 6, it is characterized in that: described thermal source is one to be arranged at respectively the well heater of the bottom of described first, second and third purifying groove, and all wall temperatures of described first, second and third purifying groove are to control by a thermostatted that is coated on respectively described first, second and third purifying groove perisporium.
8. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, is characterized in that: described melt temperature is between 380 ℃ to 550 ℃.
9. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, is characterized in that: described the first temperature is between 340 ℃ to 350 ℃.
10. the method for continuous batch of purifying saltpetre in the waste producing from glass sclerosis processing procedure as claimed in claim 1, is characterized in that: described the second temperature is between 333 ℃ to 340 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210235093.7A CN103539167B (en) | 2012-07-09 | 2012-07-09 | Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210235093.7A CN103539167B (en) | 2012-07-09 | 2012-07-09 | Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103539167A true CN103539167A (en) | 2014-01-29 |
| CN103539167B CN103539167B (en) | 2015-07-15 |
Family
ID=49963089
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210235093.7A Active CN103539167B (en) | 2012-07-09 | 2012-07-09 | Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103539167B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3939292A (en) * | 1970-09-28 | 1976-02-17 | Technovation, Inc. | Process for stable phase III potassium nitrate and articles prepared therefrom |
| JPH0933688A (en) * | 1995-07-18 | 1997-02-07 | Mitsubishi Materials Corp | Recovery method for uranium oxide |
| CN1559904A (en) * | 2004-02-25 | 2005-01-05 | 中国建筑材料科学研究院 | Purification process of potassium nitrate for producing chemical toughened glass |
| CN101182014A (en) * | 2007-12-15 | 2008-05-21 | 文水县振兴化肥有限公司 | Preparation technique of potassium nitrate |
| KR20110017128A (en) * | 2009-08-13 | 2011-02-21 | 주식회사 싸나켐 | The potassium nitrate manufacturing method which uses of etching waste solution |
| CN102137958A (en) * | 2008-08-29 | 2011-07-27 | 住友大阪水泥股份有限公司 | Thallium and potassium nitrate recovery method and recovery apparatus |
| TW201309592A (en) * | 2011-08-16 | 2013-03-01 | Univ Nat Formosa | Method for purifying potassium nitrate from waste produced during the glass curing process |
-
2012
- 2012-07-09 CN CN201210235093.7A patent/CN103539167B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3939292A (en) * | 1970-09-28 | 1976-02-17 | Technovation, Inc. | Process for stable phase III potassium nitrate and articles prepared therefrom |
| JPH0933688A (en) * | 1995-07-18 | 1997-02-07 | Mitsubishi Materials Corp | Recovery method for uranium oxide |
| CN1559904A (en) * | 2004-02-25 | 2005-01-05 | 中国建筑材料科学研究院 | Purification process of potassium nitrate for producing chemical toughened glass |
| CN101182014A (en) * | 2007-12-15 | 2008-05-21 | 文水县振兴化肥有限公司 | Preparation technique of potassium nitrate |
| CN102137958A (en) * | 2008-08-29 | 2011-07-27 | 住友大阪水泥股份有限公司 | Thallium and potassium nitrate recovery method and recovery apparatus |
| KR20110017128A (en) * | 2009-08-13 | 2011-02-21 | 주식회사 싸나켐 | The potassium nitrate manufacturing method which uses of etching waste solution |
| TW201309592A (en) * | 2011-08-16 | 2013-03-01 | Univ Nat Formosa | Method for purifying potassium nitrate from waste produced during the glass curing process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103539167B (en) | 2015-07-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102956936B (en) | Method for treating lithium iron phosphate cathode material of waste and old power lithium battery of automobile | |
| CN100593041C (en) | Method and system for reclaiming valuable resource in acidic etching waste liquid | |
| CN103014775B (en) | A kind of fused salt electrolysis process produces method and the device of titanium | |
| US8956424B2 (en) | Method and apparatus for sequencing-batch purification of potassium nitrate from solid waste produced by glass-strengthening process | |
| CN105200248B (en) | A kind of step of utilization carbide slag one neutralizes the method that titanium white waste acid prepares high-purity scandium | |
| CN102492848B (en) | Method for recovering NdFeB waste material by cold crucible induction smelting technology | |
| CN103014762B (en) | The raw metalliferous device of a kind of fused salt electrolysis process | |
| CN103781922A (en) | Apparatus and method for condensing metal vapor | |
| CN103539167B (en) | Method of continuously purifying potassium nitrate in batch in waste generated by glass hardening process | |
| CN202729826U (en) | Equipment for purifying potassium nitrate in waste generated in glass gardening process | |
| CN104711577A (en) | Copper and copper alloy workpiece chemical polishing working solution and production method thereof | |
| Chen et al. | Research status of recovery of indium from indium-tin oxide (ITO) targets | |
| CN102874772A (en) | Method for preparing high-purity tellurium by using tellurium dioxide | |
| CN103993179A (en) | Method for recovering germanium from germanium-silicon alloy | |
| CN108751188A (en) | A kind of graphite purification method | |
| CN103484679A (en) | Method for recycling tin and copper from waste tinned copper needles | |
| CN107986303A (en) | The technique that a kind of lepidolite removal of impurities slag recycling prepares lithium carbonate | |
| TWI411579B (en) | A method for purifying potassium nitrate from waste from the glass hardening process | |
| CN103159244A (en) | Method for production of sodium aluminum fluoride | |
| CN106947873A (en) | A kind of method for removing impurity lead in thick bismuth alloy | |
| CN109594088A (en) | The stripping liquid and preparation method and obstacles in quit of titanium nitride or TiAlN film layer | |
| KR20050024469A (en) | Application of neutralization titration for “method for treating of etching waste acid” | |
| CN101041521A (en) | H acid waste water by natrium chloratum addition process | |
| CN216404109U (en) | Device for improving yield of cooling pure water for copper pipe | |
| CN113089021B (en) | Method for recycling waste in sulfur hexafluoride production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |