CN102134097A - Separating device of chromate - Google Patents
Separating device of chromate Download PDFInfo
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- CN102134097A CN102134097A CN2011100352276A CN201110035227A CN102134097A CN 102134097 A CN102134097 A CN 102134097A CN 2011100352276 A CN2011100352276 A CN 2011100352276A CN 201110035227 A CN201110035227 A CN 201110035227A CN 102134097 A CN102134097 A CN 102134097A
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- chromic salt
- bucket
- chromate
- liquid phase
- oxidation reaction
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Abstract
The invention provides a separating device of chromate. In a continuous liquid phase oxidation reaction tower, mixture of chromate prepared by reaction flows into a low storage barrel added with sodium hydroxide (potassium hydroxide) solution; after being stirred uniformly, the mixture is pumped into a solid-liquid separator; and by solid-liquid separation, the purpose of separating sodium hydroxide (potassium hydroxide) from the chromate is achieved; and the separating device has the advantages that the separating effect is good, the separating technique is simple and continuous, the labor intensity of workers is reduced and the production cost is low and the like, and the separating device can be widely used for separation of the chromate.
Description
Technical field
The invention belongs to the production of the mineral compound of chromium, say so in more detail about the tripping device of chromic salt.
Background technology
Produce the device of chromic salt at present both at home and abroad, generally be to adopt the open hearth roasting method to produce chromic salt, in the production equipment process of chromic salt, because the influence of impurity in the chromite ore fine, so in the separating technology process of chromic salt, the separation of chromic salt is carried out in general employing leaching.In leaching separating technology process, weak points such as process complexity, separating impurity is incomplete, speed is slow, labor strength is big are arranged.
Present inventors, because the deficiency of above chromic salt separating technology, through long-term research with keen determination.Discovery adds sodium hydroxide (potassium) solution in the reaction mixture of chromic salt, the solubleness of chromic salt in sodium hydroxide (potassium) solution is reduced and reach isolating purpose, has so far finished the present invention.
Summary of the invention
The tripping device that the purpose of this invention is to provide a kind of chromic salt good separating effect, chromic salt that chromic salt purity is high.
Second purpose of the present invention provides a kind of tripping device of energy-conservation, chromic salt that separating technology is easy.
The 3rd purpose of the present invention provides a kind of continuous isolating tripping device that reduces labor strength, production safety, chromic salt.
In order to achieve the above object, the present invention is achieved in that
Chromic salt through continuous liquid phase oxidation reaction tower makes is characterized in that reacting the chromic salt mixture of making, and after stirring in adding has the storage bucket (41) of sodium hydroxide (potassium) solution, is evacuated in the solid-liquid separator (44) again and separates.
The tripping device of chromic salt mixture of the present invention is characterized in that the storage bucket (41) of described tripping device, is lower than the horizontal plane of the reacted material outlet of continuous liquid phase oxidation reaction tower (26) (29).
The chromic salt mixture of making through reaction in continuous liquid phase oxidation reaction tower (26) flow into low level through material outlet (29) and stores in the bucket (41), and storing interior sodium hydroxide (potassium) strength of solution of bucket (41) is the 20-45% mass percent concentration.
Wherein the mass ratio of chromic salt mixture and sodium hydroxide (potassium) solution is 1: 2.5～4.5
Description of drawings
Accompanying drawing 1 is a structure iron of the present invention
Accompanying drawing 2 is structure iron of continuous liquid phase oxidation reaction device of the present invention
1. induced draft fan; 2. flue gas outlet; 3. the chromium powder slurry outlet that is mixed; 4 chromium powder mixed ingredients slurry inlets; 5. chromium powder preheating bucket; 6. alkali lye preheating bucket; 7. flue gas outlet; 8. alkali lye import; 9. agitator; 10. alkali lye outlet; 11. pre-thermal jacket; 12. stack gas import; 13. secondary kitchen range cleaning apparatus; 14. secondary kitchen range reciprocating furnace flue gas outlet; 15. secondary kitchen range; 16. reciprocating furnace; 17. secondary pot 1; 18. secondary pot 2; 19. main kitchen range; 20. reciprocating furnace; 21. main pot 1; 22. main pot 2; 23. main kitchen range reciprocating furnace flue gas outlet; 24. main kitchen range cleaning apparatus; 25. reaction mass alkali lye import; 26. continuous liquid phase oxidation reaction tower; 27. heat required chuck outward; 28. stack gas import; 29. reacted material outlet; 30. participate in the gas feed of reaction; 31. tapered tower tray; 32. flue gas outlet; 33. reaction mass chromium powder import; 34. reaction back pneumatic outlet; 35. air preheater; 36. air intlet; 37. reacted gas feed; 38. pneumatic outlet; 39. material outlet; 40. gas-liquid separator; 41. store bucket; 42. material inlet; 43. material outlet; 44. separator; 45. material outlet; 46. separator stack gas import; 47. the pre-thermal jacket of separator; 48. material inlet; 49. material outlet; 50. separator flue gas outlet; 51. rare bucket; 52. mix the powder container.
Below in conjunction with accompanying drawing, the present invention is given further instruction by embodiment.
At first be preheating to 350 ℃ 11 tons of concentrated sodium hydroxides from the cat head opening for feed (25) of continuous liquid phase oxidation reaction tower (26) input, drop into 18 tons of mixed ingredients being preheating to 50～200 ℃ from opening for feed (33), opening for feed (30) is introduced and is preheating to 180 ℃ compression cleaned air at the bottom of the continuous liquid phase oxidation reaction tower, makes the tower internal pressure reach 0.45～0.8Mpa; Dust separating stack gas is fed continuous liquid phase oxidation reaction tower heating jacket (28), make reaction remain on 250～300 ℃ of temperature, react after 3 hours, begin drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower Sodium chromate content and be 28.05% mixture, get these 1000 kilograms, mixture flows automatically to low level through the piping step and stores in the bucket (41), 2000 kilograms of mass concentrations of adding are 45% sodium hydroxide solution in low level storage bucket (41), back being pumped in the solid-liquid separation reactor (44) with pump that stir separated, alkali lye after the separation is discharged from discharge port (49), Sodium chromate is discharged from discharge port (45), obtains 245 kilograms of Sodium chromates.
Embodiment 2
Get drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower Sodium chromate content and be 1000 kilograms in 31.23% mixture, store in the bucket (41) to low level through pipeline self, 2600 kilograms of mass concentrations of adding are 35% sodium hydroxide solution in low level storage bucket (41), after stirring, be pumped in the solid-liquid separation reactor (44) with pump and separate, alkali lye after the separation and Sodium chromate are discharged from discharge port (49) and (45) respectively, obtain 289 kilograms of Sodium chromates.
Embodiment 3
Get drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower Sodium chromate content and be 4500 kilograms in 35.83% mixture, store in the bucket (41) to low level through pipeline self, 842 kilograms of mass concentrations of adding are 20% sodium hydroxide solution in low level storage bucket (41), after stirring, be pumped in the solid-liquid separation reactor (44) with pump and separate, alkali lye after the separation and Sodium chromate are discharged from discharge port (49) and (45) respectively, obtain 339 kilograms of Sodium chromates.
Embodiment 4
At first be preheating to 350 ℃ 13.5 tons in dense potassium hydroxide from the cat head opening for feed (25) of continuous liquid phase oxidation reaction tower (26) input, drop into 18 tons of mixed ingredients being preheating to 50～200 ℃ from opening for feed (33), opening for feed (30) is introduced and is preheating to 180 ℃ compression cleaned air at the bottom of the continuous liquid phase oxidation reaction tower, makes the tower internal pressure reach 0.45～0.8Mpa; Dust separating stack gas is fed continuous liquid phase oxidation reaction tower heating jacket (28), make reaction remain on 250～300 ℃ of temperature, react after 3 hours, begin drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower potassiumchromate content and be 32.81% mixture, get these 1000 kilograms, mixture flows automatically to low level through the piping step and stores in the bucket (41), 2000 kilograms of mass concentrations of adding are 45% potassium hydroxide solution in low level storage bucket (41), back being pumped in the solid-liquid separation reactor (44) with pump that stir separated, alkali lye after the separation is discharged from discharge port (49), potassiumchromate is discharged from discharge port (45), obtains 312 kilograms of potassiumchromates.
Embodiment 5
Get drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower potassiumchromate content and be 1000 kilograms in 35.69% mixture, store in the bucket (41) to low level through pipeline self, 2600 kilograms of mass concentrations of adding are 35% potassium hydroxide solution in low level storage bucket (41), after stirring, be pumped in the solid-liquid separation reactor (44) with pump and separate, alkali lye after the separation and potassiumchromate are discharged from discharge port (49) and (45) respectively, obtain 339 kilograms of potassiumchromates.
Embodiment 6
Get drain hole (29) goes out continuously at the bottom of the continuous liquid phase oxidation reaction tower potassiumchromate content and be 1000 kilograms in 33.72% mixture, store in the bucket (41) to low level through pipeline self, 4500 kilograms of mass concentrations of adding are 20% potassium hydroxide solution in low level storage bucket (41), after stirring, be pumped in the solid-liquid separation reactor (44) with pump and separate, alkali lye after the separation and potassiumchromate are discharged from discharge port (49) and (45) respectively, obtain 320 kilograms of potassiumchromates.
The present invention has the separate chromium hydrochlorate effective, and impurity is few, and separating technology is easy, save the energy, easily operation reduces labor strength, raise labour productivity and production security, the advantages such as separation of carrying out chromate that can serialization can be widely used in the separation of chromate.
Claims (4)
1. the tripping device of a chromic salt is characterized in that the chromic salt mixture made through continuous liquid phase oxidation reaction tower, after stirring in adding has the storage bucket (41) of sodium hydroxide (potassium) solution, is evacuated in the solid-liquid separator (44) again and separates.
2. the tripping device of a kind of chromic salt according to claim 1 is characterized in that the storage bucket (41) of described tripping device, is lower than the horizontal plane of the reacted material outlet of continuous liquid phase oxidation reaction tower (26) (29).
3. the tripping device of a kind of chromic salt according to claim 1, it is characterized in that reacting the chromic salt mixture of making through continuous liquid phase oxidation reaction tower (26), flow into low level through material outlet (29) and store in the bucket (41), sodium hydroxide (potassium) strength of solution of storing in the bucket (41) is the 20-45% concentration expressed in percentage by weight.
4. the tripping device of chromic salt according to claim 1 is characterized in that storing in the bucket (41), and the solution quality ratio of the mixture of chromic salt and sodium hydroxide (potassium) is 1: 2～4.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100352276A CN102134097A (en) | 2011-01-27 | 2011-01-27 | Separating device of chromate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100352276A CN102134097A (en) | 2011-01-27 | 2011-01-27 | Separating device of chromate |
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| CN102134097A true CN102134097A (en) | 2011-07-27 |
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| CN2011100352276A Pending CN102134097A (en) | 2011-01-27 | 2011-01-27 | Separating device of chromate |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1316384A (en) * | 2001-01-21 | 2001-10-10 | 重庆嘉陵化学制品有限公司 | Process for preparing potassium permanganate with pneumatic fluidized tower |
| CN101508466A (en) * | 2008-10-24 | 2009-08-19 | 天津派森科技有限责任公司 | High-efficiency, energy-conservation and clean method for producing chromate |
| CN101659444A (en) * | 2008-08-27 | 2010-03-03 | 中国科学院过程工程研究所 | Clean production method for preparing sodium chromate from chromite |
| CN101746832A (en) * | 2009-12-29 | 2010-06-23 | 重庆昌元化工有限公司 | Potassium manganate separation technology and device |
-
2011
- 2011-01-27 CN CN2011100352276A patent/CN102134097A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1316384A (en) * | 2001-01-21 | 2001-10-10 | 重庆嘉陵化学制品有限公司 | Process for preparing potassium permanganate with pneumatic fluidized tower |
| CN101659444A (en) * | 2008-08-27 | 2010-03-03 | 中国科学院过程工程研究所 | Clean production method for preparing sodium chromate from chromite |
| CN101508466A (en) * | 2008-10-24 | 2009-08-19 | 天津派森科技有限责任公司 | High-efficiency, energy-conservation and clean method for producing chromate |
| CN101746832A (en) * | 2009-12-29 | 2010-06-23 | 重庆昌元化工有限公司 | Potassium manganate separation technology and device |
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Application publication date: 20110727 |