CN215249599U - Ammonia recovery system of ternary precursor waste water - Google Patents
Ammonia recovery system of ternary precursor waste water Download PDFInfo
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- CN215249599U CN215249599U CN202023229825.0U CN202023229825U CN215249599U CN 215249599 U CN215249599 U CN 215249599U CN 202023229825 U CN202023229825 U CN 202023229825U CN 215249599 U CN215249599 U CN 215249599U
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Abstract
The utility model discloses an ammonia recovery system of ternary precursor waste water, including ammonia still, condenser, aqueous ammonia concentration tower and tail gas absorption tower, ammonia still top is connected with the condenser, the condenser is connected with aqueous ammonia concentration tower, aqueous ammonia concentration tower top is connected with the tail gas absorption tower, the condenser lower part be connected with aqueous ammonia reflux drum, the lower part that the aqueous ammonia stream was received the jar is connected with ammonia still, the top of aqueous ammonia reflux drum is connected with aqueous ammonia concentration tower; the bottom of the ammonia water concentration tower is connected with an ammonia distillation water tank, and the top of the ammonia distillation water tank is connected with the ammonia water concentration tower. The utility model discloses a send into the waste gas of backward flow jar and ammonia still water jar the aqueous ammonia concentration tower and retrieve, reduced the replacement frequency of tail gas absorption tower absorption liquid, tail gas up to standard emission of tail gas absorption tower top emission has realized the zero release of ammonia.
Description
Technical Field
The utility model relates to a processing field of ternary precursor waste water, especially an ammonia recovery system of ternary precursor waste water.
Background
At present, the lithium ion battery occupies a larger market share in the field of wide portable electronic equipment by virtue of the advantages of high specific capacity, long cycle life, low self-discharge rate, no memory effect, environmental friendliness and the like, and is generally recognized as the most development potential power battery for the electric vehicle. The ternary nickel-cobalt-manganese positive electrode material is an important lithium ion battery positive electrode material, has the important advantages of better performance than lithium cobaltate, lower cost than lithium cobaltate, higher energy density than lithium iron phosphate and the like, and gradually becomes a mainstream positive electrode material of an automobile power battery.
In the preparation process of the anode material, the preparation process of the precursor accounts for 60%, and the quality of the precursor directly influences the performance of the anode material. The common ternary cathode material is prepared by mixing and calcining secondary spherical particles formed by agglomeration of fine grains of nickel-cobalt-manganese hydroxide and lithium hydroxide. At present, the production of ternary precursor mainly adopts coprecipitation method, i.e. nickel salt, cobalt salt, manganese salt or aluminium salt is prepared into salt solution according to a certain proportion, nickel hydroxide cobalt manganese \ aluminium precipitate is formed under the condition of alkali liquor and complexing agent, and then the qualified product is obtained through the steps of centrifugal washing, slurrying, drying and the like. In the production of the ternary precursor material, the waste water in the production process mainly comprises mother liquor and washing water generated in the synthesis reaction, aging and washing working sections, and the waste water contains pollution factors such as ammonia nitrogen, alkali, heavy metals (nickel, cobalt, manganese) and the like.
At present, the methods for treating ammonia-containing wastewater mainly comprise: steam stripping recovery or high-altitude discharge, direct evaporation, ion exchange recovery, breakpoint chlorination or biological nitrification. Among them, ion exchange recovery and breakpoint chlorination are rarely used because of their disadvantages such as high investment and high treatment cost. The direct evaporation method is a commonly used wastewater treatment method in the field of ternary precursors, ammonia nitrogen in wastewater is separated from water in the form of molecular ammonia by adopting an ammonia still, and other small amount of metal ions in the solution, such as cobalt, nickel, manganese and the like, are suspended in the solution in the form of hydroxides to be used as deamination mother liquor for further treatment. Gas enters a condenser to carry out heat exchange cooling with circulating cooling water, and is finally recovered in the form of ammonia water, non-condensable gas after heat exchange enters an ammonia water concentration tower to be further concentrated to obtain qualified ammonia water, and the non-condensable gas in the system enters a tail gas absorption tower to be absorbed by sulfuric acid to obtain an ammonium sulfate product. The method has the advantages of low ammonia water recovery rate, large load of the tail gas absorption tower, unqualified tail gas emission and increased use cost of sulfuric acid.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that an improve the ammonia recovery rate, realize the ammonia recovery system of the ternary precursor waste water of tail gas discharge to reach standard is provided.
The utility model provides a technical scheme that its technical problem adopted is: the ammonia recovery system for the ternary precursor wastewater comprises an ammonia still, a condenser, an ammonia water concentration tower and a tail gas absorption tower, wherein the top of the ammonia still is connected with the condenser, the condenser is connected with the ammonia water concentration tower, the top of the ammonia water concentration tower is connected with the tail gas absorption tower, the lower part of the condenser is connected with an ammonia water reflux tank, the lower part of the ammonia water reflux tank is connected with the ammonia still, and the top of the ammonia water reflux tank is connected with the ammonia water concentration tower; the bottom of the ammonia water concentration tower is connected with an ammonia distillation water tank, and the top of the ammonia distillation water tank is connected with the ammonia water concentration tower.
Furthermore, the ammonia water concentration tower is provided with a pure water inlet, the ammonia water concentration tower is connected with the ammonia evaporation water tank through a delivery pump, and an outlet of the delivery pump is connected with the ammonia water concentration tower.
Further, the outlet of the delivery pump is respectively connected with the middle part and the upper part of the ammonia water concentration tower.
Further, a pure water inlet and an absorption liquid inlet are formed in the tail gas absorption tower, and a tail gas discharge port is formed in the top of the tail gas absorption tower; the tail gas absorption tower bottom is connected with ammonium sulfate mother liquor pond through mother liquor delivery pump, the export of mother liquor delivery pump is connected with the upper portion and the middle part of tail gas absorption tower.
Furthermore, the bottom of the ammonia still is connected with a reboiler, and the reboiler is provided with a steam inlet, a condensed water outlet and a deamination mother liquor outlet.
The utility model has the advantages that: the utility model discloses a send into the waste gas of backward flow jar and ammonia still water jar the aqueous ammonia concentration tower and retrieve, reduced the replacement frequency of tail gas absorption tower absorption liquid, tail gas up to standard emission of tail gas absorption tower top emission has realized the zero release of ammonia.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
labeled as: the system comprises a 1-ammonia still, a 2-condenser, a 3-ammonia water concentration tower, a 31-transfer pump, a 32-pure water inlet, a 4-tail gas absorption tower, a 41-mother liquor transfer pump, a 42-tail gas discharge outlet, a 43-pure water inlet, a 44-absorption liquid inlet, a 45-mother liquor transfer pump outlet, a 5-ammonia water reflux tank, a 6-ammonia still ammonia water tank, a 61-ammonia still ammonia water tank ammonia water outlet, a 7-reboiler, a 71-condensed water outlet, a 72-steam inlet, a 73-deamination mother liquor outlet and an 8-mother liquor pool.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
Example (b):
as shown in fig. 1, the ammonia recovery system for ternary precursor wastewater comprises an ammonia still 1, a condenser 2, an ammonia water concentration tower 3 and a tail gas absorption tower 4, wherein the top of the ammonia still 1 is connected with the condenser 2, the condenser 2 is connected with the ammonia water concentration tower 3, the top of the ammonia water concentration tower 3 is connected with the tail gas absorption tower 4, the lower part of the condenser 2 is connected with an ammonia water reflux tank 5, the lower part of the ammonia water reflux tank 5 is connected with the ammonia still 1, and the top of the ammonia water reflux tank 5 is connected with the ammonia water concentration tower 3; the bottom of the ammonia water concentration tower 3 is connected with an ammonia distillation water tank 6, and the top of the ammonia distillation water tank 6 is connected with the ammonia water concentration tower 3.
The ammonia water concentration tower 3 is provided with a pure water inlet 32, the ammonia water concentration tower 3 is connected with the ammonia distillation water tank 6 through a delivery pump 31, an outlet of the delivery pump 31 is connected with the ammonia water concentration tower 3, namely, an outlet of the delivery pump 31 is connected with the middle part and the upper part of the ammonia water concentration tower 3 respectively to form a self-circulation pipeline. A pure water inlet 43 and an absorption liquid inlet 44 are arranged on the tail gas absorption tower 4, and a tail gas discharge port 42 is arranged at the top of the tail gas absorption tower 4; the bottom of the tail gas absorption tower 4 is connected with an ammonium sulfate mother liquor pool through a mother liquor delivery pump 41, and an outlet of the mother liquor delivery pump 41 is connected with the upper part and the middle part of the tail gas absorption tower 4 to form a self-circulation pipeline of the mother liquor delivery pump 41. The bottom of the ammonia still 1 is connected with a reboiler 7, and the reboiler 7 is provided with a steam inlet 72, a condensed water outlet 71 and a deamination mother liquor outlet 73.
The ternary precursor wastewater from the mother liquor pool 8 enters an ammonia still 1 through a feed pump, feed liquor at the bottom of the ammonia still 1 is heated by a reboiler 7 to generate steam, the steam enters the ammonia still 1, the steam upwards brings ammonia in the wastewater to the top of the tower in the ammonia still 1 and enters a condenser 2, low-concentration ammonia water obtained after condensation by the condenser 2 enters the ammonia still 1 through an ammonia water reflux tank 5, ammonia gas which is not condensed enters an ammonia water concentration tower 3, the ammonia water is circulated in the ammonia water concentration tower 3 through a conveying pump 31 at the bottom of the ammonia water concentration tower 3, qualified ammonia water is sent to an ammonia water tank 6 for storage and standby, and non-condensed gas in the ammonia water reflux tank 5 and the ammonia water tank 6 is sent to the ammonia water concentration tower 3 for washing and concentration; the gas in the ammonia water concentration tower 3 enters the tail gas absorption tower 4 through the top of the tower, and is absorbed by the sulfuric acid absorption liquid to obtain an ammonium sulfate product, and the non-condensable gas is discharged through a tail gas discharge port 42 at the top of the tower. When the device is used for treating the ternary precursor wastewater, the acid adding frequency of the tail gas absorption tower is reduced from 6 times per day to once per 3 days, so that the consumption of dilute sulfuric acid in absorption liquid is greatly saved, and the tail gas emission is changed from the previous ammonia emission exceeding the standard for a long time into the current zero emission.
Claims (5)
1. Ammonia recovery system of ternary precursor waste water, including ammonia still, condenser, aqueous ammonia concentration tower and tail gas absorption tower, ammonia still top is connected with the condenser, the condenser is connected with aqueous ammonia concentration tower, aqueous ammonia concentration tower top is connected with the tail gas absorption tower, its characterized in that: the lower part of the condenser is connected with an ammonia water reflux tank, the lower part of the ammonia water flow collection tank is connected with an ammonia still, and the top of the ammonia water reflux tank is connected with an ammonia water concentration tower; the bottom of the ammonia water concentration tower is connected with an ammonia distillation water tank, and the top of the ammonia distillation water tank is connected with the ammonia water concentration tower.
2. The system for recovering ammonia from ternary precursor wastewater according to claim 1, wherein: the ammonia water concentration tower is provided with a pure water inlet, the ammonia water concentration tower is connected with the ammonia distillation water tank through a delivery pump, and an outlet of the delivery pump is connected with the ammonia water concentration tower.
3. The system for recovering ammonia from ternary precursor wastewater according to claim 2, wherein: and the outlet of the delivery pump is respectively connected with the middle part and the upper part of the ammonia water concentration tower.
4. The system for recovering ammonia from ternary precursor wastewater according to claim 1, wherein: the tail gas absorption tower is provided with a pure water inlet and an absorption liquid inlet, and the top of the tail gas absorption tower is provided with a tail gas discharge port; the tail gas absorption tower bottom is connected with ammonium sulfate mother liquor pond through mother liquor delivery pump, the export of mother liquor delivery pump is connected with the upper portion and the middle part of tail gas absorption tower.
5. The system for recovering ammonia from ternary precursor wastewater according to claim 1, wherein: the bottom of the ammonia still is connected with a reboiler, and the reboiler is provided with a steam inlet, a condensed water outlet and a deamination mother liquor outlet.
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| CN202023229825.0U CN215249599U (en) | 2020-12-28 | 2020-12-28 | Ammonia recovery system of ternary precursor waste water |
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| CN202023229825.0U CN215249599U (en) | 2020-12-28 | 2020-12-28 | Ammonia recovery system of ternary precursor waste water |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
| CN115212706B (en) * | 2022-07-11 | 2023-08-18 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
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