CN105692658A - Method for recycling potassium carbonate from aluminum oxide production process - Google Patents
Method for recycling potassium carbonate from aluminum oxide production process Download PDFInfo
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- CN105692658A CN105692658A CN201610034190.8A CN201610034190A CN105692658A CN 105692658 A CN105692658 A CN 105692658A CN 201610034190 A CN201610034190 A CN 201610034190A CN 105692658 A CN105692658 A CN 105692658A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
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Abstract
The invention relates to a method for recycling potassium carbonate from an aluminum oxide production process. The method is characterized by comprising the steps that 1, a carbonation decomposition reaction is conducted on mother liquor or a stock solution decomposed through a Bayer process; 2 filtering is conducted; 3, aluminum hydroxide carbon points are washed and then sent to a flash vessel obtained after Bayer digestion for post densification digestion digestion, and a product serves either as aluminum hydroxide seeds of the decomposition procedure or as an aluminum hydroxide product; 4, carbonic acid mother liquor and aluminate hydrate wash liquor are subjected to preliminary vacuum evaporation and preliminary cooling crystallization; 5, preliminary vacuum evaporation mother liquor is subjected to secondary vacuum evaporation and secondary cooling crystallization; 6, generated sodium potassium carbonate double salt crystals are dissolved with the carbonic acid mother liquor and then sent to preliminary vacuum evaporation; 7, generated secondary vacuum evaporation mother liquor is subjected to third vacuum evaporation and third cooling crystallization; 8, obtained third vacuum evaporation mother liquor and secondary vacuum evaporation mother liquor are mixed and then subjected to third vacuum evaporation; 9, obtained potassium carbonate crystals are sintered, and the potassium carbonate is obtained. A potassium carbonate product obtained through the method is high in economic value, and adverse influences generated by K<+> accumulated in the aluminum oxide production process can be eliminated.
Description
Technical field
A kind of method reclaiming potassium carbonate from aluminum oxide production process, relates to a kind of from rich in the method reclaiming potassium carbonate the sodium aluminate solution of potassium element。
Background technology
Potassium carbonate is widely used in chemical industry, electronics, glass, pottery and medicine and other fields, is the important raw material of industry。External Potash mineral resources is mostly water solublity, and production cost is low；Domestic Potash mineral resources is that the water-insoluble potassium such as nepheline, potash feldspar is containing mineral, production procedure complexity, production cost height mostly。
The bauxite of China certain areas contains the potassium of high level, in aluminum oxide production process, potassium can accumulate gradually, can cause that analytical product granularity attenuates when it accumulates and exceed a certain critical concentration in alumina producing flow process, because containing a certain amount of potassium, in turn electrolytic aluminium process being had a negative impact simultaneously in the alumina product obtained。Such as, the K in some alumina producer circulating mother liquor2O concentration alreadys more than 100g/L through accumulation, and also has the trend constantly raised, and aluminum oxide production process creates adverse effect, and electrolytic aluminium process is also created adverse effect as the raw material of electrolytic aluminium by simultaneous oxidation aluminum product。Up to the present the K effectively suppressed in mother solution is also lacked2The O method on the impact of aluminum oxide production process, equally also lacks the method on the impact of Aluminum Electrolysis Production process of the potassium in effective inhibited oxidation aluminum。
Summary of the invention
The purpose of the present invention is aiming at the deficiency that above-mentioned prior art exists, it is provided that a kind of K that can effectively eliminate in flow process accumulation+Adverse effect to alumina producing, can obtain again the method reclaiming potassium carbonate from aluminum oxide production process with the potassium carbonate product of higher economic worth。
It is an object of the invention to be achieved through the following technical solutions。
A kind of recovery potassium carbonate method from aluminum oxide production process, it is characterised in that the step of its technical process includes:
(1), in Bayer process decomposition nut liquid or decomposition stock solution, pass into CO2Carry out carbonation decomposition reaction；
(2) reacted for carbonation decomposition serosity is filtered, obtains carbon and divide aluminium hydroxide and carbon mother liquid；
(3), after dividing aluminium hydroxide to carry out washing process in the carbon obtained, it is sent to the flash vessel after Bayer dissolution and carries out rear enrichment dissolution or the aluminium hydroxide crystal seed as decomposition process, or as aluminum hydroxide product；
(4) the aluminum hydroxide wash liquor of the carbon mother liquid of step (2) and step (3) is carried out a vacuum evaporation and the 1st decrease temperature crystalline processes and obtain crystals of sodium carbonate and a vacuum evaporation mother solution；
(5) a vacuum evaporation mother solution of step (4) is carried out secondary vacuum evaporation and the 2nd decrease temperature crystalline obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；
(6) sodium potassium carbonate double salt crystal carbon mother liquid step (5) produced send a vacuum evaporation after dissolving；
(7) the secondary vacuum mother liquid evaporation that step (5) produces is carried out three vacuum evaporation and the 3rd decrease temperature crystalline obtains potassium carbonate crystal and three vacuum evaporation mother solutions；
(8) after being mixed with secondary vacuum mother liquid evaporation by three vacuum evaporation mother solutions that step (7) obtains, carry out three vacuum evaporation；
(9) the potassium carbonate crystal that step (7) obtains is calcined, obtain potassium carbonate。
The one of the present invention reclaims potassium carbonate method from aluminum oxide production process, it is characterized in that its step (4) obtains obtaining after crystals of sodium carbonate adds lime cream causticization sodium hydroxide solution and causticization slag, causticization slag is outer row after washing, the mother liquid evaporation operation that the wash water of causticization slag and described sodium hydroxide solution returning alumina produce。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that in the described carbonation decomposition course of reaction of its step (1), the aluminium oxide in decomposition nut liquid all precipitates out with aluminium hydroxide form。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterized in that in the described carbonation decomposition reaction temperature of its step (1) be 60～75 DEG C, crystal seed coefficient is 0.05～0.35, the carbonation reaction time is 3.5～6.0h, the caustic sodium concentration 1.0～6.0g/L in carbon mother liquid during reaction end。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterized in that the carbon mother liquid of its step (2) can obtain potassium carbonate crystal after three times evaporate and process with three decrease temperature crystallines, after calcining 2h at 200 DEG C of described potassium carbonate crystal, obtain potassium carbonate product。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that the temperature of the one of described carbon mother liquid, two and three vacuum evaporation is 95～105 DEG C, the crystallization temperature after described the 1st, the 2nd and the 3rd time time cooling is 85～95 DEG C。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that when a described carbon mother liquid flush distillation terminates, gravity is more than 1.48g/cm3, when secondary and three evaporations terminate, gravity is more than 1.55g/cm3。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that the sodium potassium carbonate double salt crystal carbon mother liquid that its step (5) produces send a vacuum evaporation after dissolving。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that three the vacuum evaporation mother solutions obtained in its step (7) return after mixing with secondary vacuum mother liquid evaporation and carry out three vacuum evaporation。
A kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, it is characterised in that the crystals of sodium carbonate obtained in its step (4) obtains sodium hydroxide solution and causticization slag after adding lime cream causticization；Causticization slag is outer row after washing, the evaporization process that the wash water of causticization slag and described sodium hydroxide solution returning alumina produce。
Adopt a kind of method reclaiming potassium carbonate from aluminum oxide production process of the present invention, be possible not only to the potassium carbonate product obtaining that there is higher economic worth, and the K of accumulation in alumina producing flow process can be eliminated+Adverse effect to alumina producing。
Detailed description of the invention
A kind of method reclaiming potassium carbonate from aluminum oxide production process, it is characterised in that the step of its removal process includes:
(1) containing K+Bayer process decomposition nut liquid or decompose in stock solution, pass into the CO that volumetric concentration is 20%～38%2Carry out carbonation reaction, make the aluminium oxide in decomposition nut liquid precipitate out with aluminium hydroxide form, obtain aluminum hydroxide slurry；
(2) the aluminum hydroxide slurry that step 1 produces being filtered obtains carbon and divides aluminium hydroxide and carbon mother liquid；
(3) the flash vessel after the carbon that step 2 produces divides aluminium hydroxide be sent to Bayer dissolution after carrying out washing process carries out rear enrichment dissolution, or the aluminium hydroxide crystal seed as decomposition process, or as aluminum hydroxide product, wash water carries out a vacuum evaporation with described carbon mother liquid after mixing；
(4) the aluminium hydroxide wash water that carbon mother liquid step 2 produced and step 3 produce carries out a vacuum evaporation, is not less than 1.48g/cm when being evaporated to gravity3The 1st decrease temperature crystalline of Shi Jinhang processes and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；
(5) vacuum evaporation mother solution step 4 produced carries out secondary vacuum evaporation, is not less than 1.55g/cm when being evaporated to gravity3The 2nd decrease temperature crystalline of Shi Jinhang obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；
(6) sodium potassium carbonate double salt crystal carbon mother liquid step 5 produced send a vacuum evaporation after dissolving；
(7) secondary vacuum mother liquid evaporation step 5 produced carries out three vacuum evaporation, is not less than 1.55g/cm when being evaporated to gravity3The 3rd decrease temperature crystalline of Shi Jinhang can obtain potassium carbonate crystal and three vacuum evaporation mother solutions；
(8) three vacuum evaporation mother solutions step 7 obtained carry out three vacuum evaporation after mixing with secondary vacuum mother liquid evaporation；
(9) potassium carbonate crystal step 7 obtained can obtain the purity qualified potassium carbonate product more than 96% after calcining 2h at 200 DEG C；
(10) obtaining step 4 obtaining sodium hydroxide solution and causticization slag after crystals of sodium carbonate adds lime cream causticization, causticization slag is outer row after washing, the mother liquid evaporation operation that the wash water of causticization slag and described sodium hydroxide solution returning alumina produce。
Embodiment 1
The caustic sodium concentration Nk of Bayer process decomposition nut liquid is 160g/L, Al2O3Concentration is 95.7g/L, K2O content is the 50g/L CO passing into that when temperature 60 C concentration is 20%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.05, and the response time is 3.5h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 1.0g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 95 DEG C vacuum evaporation to gravity 1.52g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 95 DEG C vacuum evaporation to gravity 1.60g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 95 DEG C vacuum evaporation to gravity 1.60g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Embodiment 2
The caustic sodium concentration Nk of Bayer process decomposition nut liquid is 170g/L, Al2O3Concentration is 102g/L, K2O content is that 70g/L passes into, when temperature 75 DEG C, the CO that concentration is 38%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.35, and the response time is 6h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 6g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 105 DEG C vacuum evaporation to gravity 1.48g/cm3, it is cooled to 95 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 95 DEG C of crystallization 3h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 95 DEG C of crystallization 2h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Embodiment 3
The caustic sodium concentration Nk of Bayer process decomposition nut liquid is 178g/L, Al2O3Concentration is 106g/L, K2O content is the 110g/L CO passing into that when temperature 70 C concentration is 35%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.15, and the response time is 6h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 6g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 105 DEG C vacuum evaporation to gravity 1.48g/cm3, it is cooled to 95 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 95 DEG C of crystallization 2h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 95 DEG C of crystallization 4h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Embodiment 4
The caustic sodium concentration Nk of Bayer process decomposition nut liquid is 178g/L, Al2O3Concentration is 106g/L, K2O content is the 110g/L CO passing into that when temperature 70 C concentration is 20%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.15, and the response time is 6h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 3g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 105 DEG C vacuum evaporation to gravity 1.48g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 4h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Embodiment 5
The caustic sodium concentration Nk of Bayer process decomposition nut liquid is 160g/L, Al2O3Concentration is 95.7g/L, K2O content is the 40g/L CO passing into that when temperature 70 C concentration is 25%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.10, and the response time is 6h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 2g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 105 DEG C vacuum evaporation to gravity 1.48g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 4h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Embodiment 6
It is 165g/L, Al that Bayer process decomposes the caustic sodium concentration Nk of stock solution2O3Concentration is 187.0g/L, K2O content is the 40g/L CO passing into that when temperature 70 C concentration is 25%2Gas carries out carbonation reaction, and crystal seed coefficient is 0.30, and the response time is 6h, and during reaction end, the caustic sodium concentration Nk in carbon mother liquid is 2g/L, and the carbon obtained divides aluminium hydroxide strainability good；Described carbon mother liquid and carbon are divided aluminium hydroxide wash water at temperature 105 DEG C vacuum evaporation to gravity 1.48g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains crystals of sodium carbonate and a vacuum evaporation mother solution；By a described vacuum evaporation mother solution at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 4h and obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；Send carbon mother liquid vacuum evaporation operation after being dissolved by sodium potassium carbonate double salt crystal carbon mother liquid；By described secondary vacuum mother liquid evaporation at temperature 105 DEG C vacuum evaporation to gravity 1.55g/cm3, it is cooled to 85 DEG C of crystallization 2h and obtains potassium carbonate crystal and three vacuum evaporation mother solutions；Three the vacuum evaporation mother solutions obtained after being separated by described potassium carbonate crystal return in secondary vacuum mother liquid evaporation；The purity qualified potassium carbonate product more than 96% can be obtained after described potassium carbonate crystal is calcined 2h at 200 DEG C。
Claims (10)
1. one kind is reclaimed potassium carbonate method from aluminum oxide production process, it is characterised in that the step of its technical process includes:
(1), in Bayer process decomposition nut liquid or decomposition stock solution, pass into CO2Carry out carbonation decomposition reaction；
(2) reacted for carbonation decomposition serosity is filtered, obtains carbon and divide aluminium hydroxide and carbon mother liquid；
(3), after dividing aluminium hydroxide to carry out washing process in the carbon obtained, it is sent to the flash vessel after Bayer dissolution and carries out rear enrichment dissolution or the aluminium hydroxide crystal seed as decomposition process, or as aluminum hydroxide product；
(4) the aluminum hydroxide wash liquor of the carbon mother liquid of step (2) and step (3) is carried out a vacuum evaporation and the 1st decrease temperature crystalline processes and obtain crystals of sodium carbonate and a vacuum evaporation mother solution；
(5) a vacuum evaporation mother solution of step (4) is carried out secondary vacuum evaporation and the 2nd decrease temperature crystalline obtains sodium potassium carbonate double salt crystal and secondary vacuum mother liquid evaporation；
(6) sodium potassium carbonate double salt crystal carbon mother liquid step (5) produced send a vacuum evaporation after dissolving；
(7) the secondary vacuum mother liquid evaporation that step (5) produces is carried out three vacuum evaporation and the 3rd decrease temperature crystalline obtains potassium carbonate crystal and three vacuum evaporation mother solutions；
(8) after being mixed with secondary vacuum mother liquid evaporation by three vacuum evaporation mother solutions that step (7) obtains, carry out three vacuum evaporation；
(9) the potassium carbonate crystal that step (7) obtains is calcined, obtain potassium carbonate。
2. one according to claim 1 reclaims potassium carbonate method from aluminum oxide production process, it is characterized in that its step (4) obtains obtaining after crystals of sodium carbonate adds lime cream causticization sodium hydroxide solution and causticization slag, causticization slag is outer row after washing, the mother liquid evaporation operation that the wash water of causticization slag and described sodium hydroxide solution returning alumina produce。
3. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterised in that in the described carbonation decomposition course of reaction of its step (1), the aluminium oxide in decomposition nut liquid all precipitates out with aluminium hydroxide form。
4. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterized in that in the described carbonation decomposition reaction temperature of its step (1) be 60～75 DEG C, crystal seed coefficient is 0.05～0.35, the carbonation reaction time is 3.5～6.0h, the caustic sodium concentration 1.0～6.0g/L in carbon mother liquid during reaction end。
5. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterized in that the carbon mother liquid of its step (2) can obtain potassium carbonate crystal after three times evaporate and process with three decrease temperature crystallines, after calcining 2h at 200 DEG C of described potassium carbonate crystal, obtain potassium carbonate product。
6. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterized in that the temperature of the one of described carbon mother liquid, two and three vacuum evaporation is 95～105 DEG C, the described crystallization temperature after the 1st, the 2nd and the 3rd cooling is 85～95 DEG C。
7. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterised in that when a described carbon mother liquid flush distillation terminates, gravity is more than 1.48g/cm3, when secondary and three evaporations terminate, gravity is more than 1.55g/cm3。
8. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterised in that the sodium potassium carbonate double salt crystal carbon mother liquid that its step (5) produces send a vacuum evaporation after dissolving。
9. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterised in that three the vacuum evaporation mother solutions obtained in its step (7) return after mixing with secondary vacuum mother liquid evaporation and carry out three vacuum evaporation。
10. a kind of method reclaiming potassium carbonate from aluminum oxide production process according to claim 1, it is characterised in that the crystals of sodium carbonate obtained in its step (4) obtains sodium hydroxide solution and causticization slag after adding lime cream causticization；Causticization slag is outer row after washing, the evaporization process that the wash water of causticization slag and described sodium hydroxide solution returning alumina produce。
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110028087A (en) * | 2018-07-26 | 2019-07-19 | 沈阳铝镁设计研究院有限公司 | A kind of method and device of reduction system carbon alkali concentration |
| CN111874927A (en) * | 2020-06-22 | 2020-11-03 | 河南华慧有色工程设计有限公司 | Carbon method aluminum oxide energy-saving emission-reducing production method |
| CN113600010A (en) * | 2021-07-19 | 2021-11-05 | 陕西未来能源化工有限公司 | Purification and regeneration method of hot potash solution in Fischer-Tropsch synthesis tail gas, device and application thereof |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110028087A (en) * | 2018-07-26 | 2019-07-19 | 沈阳铝镁设计研究院有限公司 | A kind of method and device of reduction system carbon alkali concentration |
| CN110028087B (en) * | 2018-07-26 | 2021-08-13 | 沈阳铝镁设计研究院有限公司 | Method for reducing carbon-alkali concentration of system in alumina production process |
| CN111874927A (en) * | 2020-06-22 | 2020-11-03 | 河南华慧有色工程设计有限公司 | Carbon method aluminum oxide energy-saving emission-reducing production method |
| CN113600010A (en) * | 2021-07-19 | 2021-11-05 | 陕西未来能源化工有限公司 | Purification and regeneration method of hot potash solution in Fischer-Tropsch synthesis tail gas, device and application thereof |
| CN113600010B (en) * | 2021-07-19 | 2023-09-01 | 陕西未来能源化工有限公司 | Purification and regeneration method for Fischer-Tropsch synthesis tail gas hot potash solution, device and application thereof |
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