CN106865724A - The processing method of tantalum and niobium hydrometallurgy raffinate and comprehensive wastewater - Google Patents
The processing method of tantalum and niobium hydrometallurgy raffinate and comprehensive wastewater Download PDFInfo
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- CN106865724A CN106865724A CN201710190682.0A CN201710190682A CN106865724A CN 106865724 A CN106865724 A CN 106865724A CN 201710190682 A CN201710190682 A CN 201710190682A CN 106865724 A CN106865724 A CN 106865724A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
- C02F2101/14—Fluorine or fluorine-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
Abstract
The processing method of a kind of tantalum and niobium hydrometallurgy raffinate and comprehensive wastewater, belongs to field of waste water treatment.Raffinate processing method includes proceeding as follows raffinate：PH value to 7 7.5 formation precipitations is adjusted with ammonia or ammoniacal liquor, is separated for the first time.With sulphur acid for adjusting pH value to 56, precipitation, second separation are formed in the presence of aluminium salt and sodium salt.PH value is adjusted to more than 12 with calcium hydroxide, and precipitation and separation obtains treatment fluid.It carries out separating and recovering the treatment for realizing sewage to the valuable material in raffinate with precipitation form, realizes the recycling of resource；Improvement amount is reduced simultaneously, and treatment is thorough.Integrated waste water treatment method includes as stated above processing raffinate, and the alkaline waste water mixed processing that the treatment fluid that will be obtained is produced with tantalum and niobium hydrometallurgy.By the main treatment fluid containing ammonium ion and the alkaline waste water mixed processing containing a large amount of ammonium ions, technique is saved, it is simple to operate.
Description
Technical field
It is in particular to a kind of tantalum and niobium hydrometallurgy raffinate and comprehensively useless the present invention relates to field of waste water treatment
The processing method of water.
Background technology
The technique that tantalum and niobium hydrometallurgy is carried out using ammonia, sulfuric acid, hydrofluoric acid, it is residual containing acid extraction after its extraction pickling tantalum niobium
Liquid contains substantial amounts of fluorine ion, sulfate ion and valuable metal.Specifically, the content of wherein sulfuric acid is about 30wt%, hydrogen fluorine
The content of acid is about 4-8wt%, and the content of metallic salt is about 2-4wt%.Prior art is logical to the treatment containing acid extraction raffinate
Neutralization precipitation is carried out frequently with lime stone, by harmful substance and metal ion concentration in solid phase, then separation of solid and liquid is carried out, water phase
Discharged again after up to standard.
Because the output of industrial tantalum niobium raffinate is big, and traditional processing method raffinate per ton need to be consumed about
1200kg lime stones, will be gathered in solid phase containing harmful substance and valuable metal ions in acid extraction raffinate etc., process raw material
Demand is big, and generates substantial amounts of solid waste.And a large amount of solid waste directly discharge and environment can be impacted, one need to be entered
Step treatment is discharged again, increased the difficulty and cost for the treatment of.Additionally, the processing method can not realize the thorough place of waste
Reason, and the valuable materials such as valuable metal and acid ion in raffinate cannot be recycled, it is impossible to realize the abundant of resource
Utilize.
The content of the invention
It is an object of the invention to provide a kind of processing method of tantalum and niobium hydrometallurgy raffinate, it is in raffinate
Valuable material reclaimed to realize the treatment of sewage, realize the recycling of resource；Improvement amount is reduced simultaneously, is processed
Thoroughly.
It is another object of the present invention to provide a kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, it will be completed
The raffinate that valuable material is reclaimed is mixed in alkaline waste water and handles together, process is simple.
What embodiments of the invention were realized in：
A kind of processing method of tantalum and niobium hydrometallurgy raffinate, it includes proceeding as follows raffinate：
PH value is adjusted with ammonia or ammoniacal liquor and form precipitation to 7-7.5, separate for the first time；With sulphur acid for adjusting pH value to 5-6,
Precipitation, second separation are formed in the presence of aluminium salt and sodium salt；PH value is adjusted to more than 12 with calcium hydroxide, and precipitation and separation must be processed
Liquid.
A kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, it includes using above-mentioned tantalum and niobium hydrometallurgy extraction residual
The disposal methods raffinate of liquid, then the alkaline waste water that the treatment fluid that will be obtained is produced with tantalum and niobium hydrometallurgy mixes.
The beneficial effect of the embodiment of the present invention is：
The present invention provide tantalum and niobium hydrometallurgy raffinate processing method, with ammonia adjust pH value to 7-7.5 when, tungsten from
Son reaction forms ammonium paratungstate, and ammonium paratungstate is almost insoluble in the pH value range, can be separated with precipitation form.Aluminium salt and sodium salt
React to form cryolite precipitation with fluorine ion, the separation of fluorine ion is realized in second separation.Sulfate radical and calcium hydroxide reaction
The calcium sulfate precipitation that generation is easily isolated.The processing method leads to the tungsten ion in raffinate, fluorine ion and sulfate ion
The mode for crossing formation precipitation is separated successively, is easy to be separately separated realization again to its tungsten ion, fluorine ion and sulfate ion
Utilize.
The alkaline waste water that tantalum and niobium hydrometallurgy is produced is to contain the molten of high concentration fluorine ion, sulfate ion and ammonium ion
Liquid.Raffinate completes mainly to contain ammonium ion in treatment fluid in the solution after reclaimer operation, and the tantalum niobium that the present invention is provided is wet
Method smelts the processing method of comprehensive wastewater, and treatment fluid is mixed with the alkaline waste water, without individually being processed treatment fluid again,
It is simple to operate.
Specific embodiment
To make the purpose, technical scheme and advantage of the embodiment of the present invention clearer, below will be in the embodiment of the present invention
Technical scheme be clearly and completely described.Unreceipted actual conditions person, builds according to normal condition or manufacturer in embodiment
The condition of view is carried out.Agents useful for same or the unreceipted production firm person of instrument, are the conventional product that can be obtained by commercially available purchase
Product.
Tantalum and niobium hydrometallurgy raffinate and the processing method of comprehensive wastewater below to the embodiment of the present invention is carried out specifically
Explanation.
Raffinate be tantalum and niobium hydrometallurgy technique in, extraction pickling tantalum niobium after acid-bearing wastewater, containing substantial amounts of fluorine from
Son, sulfate ion and valuable metal ions such as tungsten ion, iron ion etc..
The present invention provide tantalum and niobium hydrometallurgy raffinate processing method, including to raffinate carry out reclaim tungsten from
Son, the operation for reclaiming fluorine ion and recovery sulfate ion.
Because raffinate output industrially is big, therefore preferably, before the operation of tungsten ion reclaim, incite somebody to action
Raffinate is diffused dialysis treatment and is separated off sour clear liquid using pellicle etc., then carries out tungsten ion, fluorine to remaining liq
The recovery of ion and sulfate ion.Because remaining raffinate is strong brine high after separating acid clear liquid.The operation is to extraction
Raffinate is concentrated, and reduces treating capacity.
Further, main sulfur acid and hydrofluoric acid in sour clear liquid, are neutralized using magnesium hydroxide in the present invention to it.
Fluorine ion can form fluorination magnesium precipitate with magnesium ion, be recycled after separation and contain sulphur in the solution after commercial Application, separation of solid and liquid
Sour magnesium, the magnesium ion in magnesium sulfate can continue on for the treatment of sour clear liquid, reduce the consumption of magnesium hydroxide.
Because solubility of the ammonium paratungstate in the water that temperature is 17 DEG C, pH value is 7.3 is minimum, about 0.064g.Returning
Receive in the operation of tungsten ion, the pH value of the raffinate that will be gone after deacidification clear liquid using ammonia or ammoniacal liquor is adjusted during to about 7-7.5,
Ammonia is dissolved in after water and the ammonium paratungstate of tungsten ion generation is practically insoluble in water and exists in the form of precipitating, ammonium paratungstate precipitation
And other metal ions formed precipitation composition tungstenic precipitation and carry out first time separation, separation of solid and liquid with realize tungsten ion with
The separation of raffinate.
Further, the solubility due to ammonium paratungstate in alkaline solution is larger, by the precipitation of the tungstenic in the present invention
It is mixed in ammoniacal liquor, or ammonium paratungstate is placed in water and to ammonia is passed through in water, ammonium paratungstate is dissolved in the water and other gold
Category ion precipitation is separated.Tungsten ion is primarily present in filtrate after separation of solid and liquid, and calcining after the filtrate evaporative crystallization can be obtained
Tungstic acid product.
In preferred embodiments of the present invention, control calcining is carried out under conditions of 873-973K, and its calcining effect is good.
Tungstic acid be widely used in produce hard alloy, manufacture tungsten filament, tungsten electrode, for shielding material, colouring agent and
Coating etc., is widely used.The operation of the recovery tungsten realizes recycling for tungsten in raffinate, and simple to operate.
For the first time separation and recovery tungsten ion operation after the completion of raffinate in mainly contain fluorine ion, sulfate ion and
Ammonium ion.In the operation for reclaiming fluorine ion, the pH value of raffinate is adjusted to 5-6 using sulfuric acid, be easy to raffinate
In fluorine ion reacted with sodium salt and aluminium salt and generate cryolite precipitation, i.e. ice crystal carries out second separation to fluorine ion
Reclaimed.
The regulation of pH is carried out using sulfuric acid, is prevented from introducing other impurity.Further, the operation of fluorine ion is reclaimed
In sodium salt use sodium sulphate, aluminium salt uses aluminum sulfate.Sodium salt and aluminium salt use sulfate, and it can avoid introducing other
Impurity, and degree of ionization in water is high.
Due to the amount of the material of fluorine ion in cryolite：The amount of aluminum ions material：The amount of the material of sodium ion is 6:
1:3, in order that the fluorine ion in raffinate is fully reacted with the sodium salt and aluminium salt for adding, the sodium salt provided in the present invention
And the amount of the material of aluminium salt is 1-1.2 times, preferably 1.1 times of amount of calculation.I.e. in sodium salt in the inventory of sodium ion, aluminium salt
The ratio between amount of material of fluorine ion is 3-3.6 in aluminum ions inventory and raffinate:1-1.2:6, more excellent is 3.3:
1.1:6。
Further, due to adding excessive aluminium salt and sodium salt in the operation for reclaiming fluorine ion, and aluminum ions presence
The purity of calcium sulfate precipitation can be influenceed, therefore before reclaiming sulfate radical after being separated at second and with calcium hydroxide, with ammonia or ammonia
The pH value of water regulation raffinate forms the precipitation for containing aluminium to 8.5-9.5, for removing the aluminium ion in raffinate.Meanwhile,
The precipitation containing aluminium of generation is circularly used in the operation for reclaim fluorine ion, reduces the consumption of aluminum sulfate.
With calcium hydroxide regulation raffinate to pH value to more than 12, sulfate radical and calcium ion in the reclaimer operation of sulfate radical
Calcium sulfate is formed, POV calcium is obtained to residue washing drying after separation of solid and liquid.
It should be noted that separate for the first time and separate for second to be only used for distinguishing lock out operation twice, separation is not represented
Sequencing.
The present invention provide tantalum and niobium hydrometallurgy comprehensive wastewater processing method, will reclaim complete tungsten ion, fluorine ion and
The alkaline waste water that the remaining treatment fluid of sulfate ion is produced with tantalum and niobium hydrometallurgy mixes and is processed in the lump.
Raffinate mainly contains ammonium after the operation for completing tungsten ion, fluorine ion and sulfate ion in its treatment fluid
Radical ion and sodium ion.Due to the alkaline waste water of tantalum and niobium hydrometallurgy contain substantial amounts of fluorine ion, ammonium ion and sulfate radical from
Son, the concentration of ammonium ion is about 25000mg/L, and the concentration of fluorine ion is about 20000mg/L, and its discharge standard be ammonium root from
Concentration≤the 15mg/L of son, fluorinion concentration≤10mg/L, therefore it is must grasp in alkaline waste water processing procedure that it removes ammonium operation
Make.The raffinate after recycling is mixed to form into mixed liquor with the alkaline waste water to be processed in the lump, without to completing back
The raffinate after making of bringing drill to an end is carried out individually except ammonium is operated, process is simple.
Further, the pH value of mixed liquor is adjusted to 9.5-10.5 with NaOH in the present invention, can be now released
Ammonia.Ammonia is reclaimed using ammonia absorption system, it is real during the ammonia of recovery can be used to reclaim tungsten and reclaim the operation of aluminium
Recycling for existing ammonium, reduces raffinate processing cost.
Preferably, due to containing substantial amounts of fluorine ion and sulfate ion in mixed liquor, may be recovered.And alkaline waste water
In contain metal ion, therefore further be filtered to remove precipitation by metallic ion after ammonia is reclaimed.Take filtrate and remove ammonium through deammoniation tower
Afterwards, sodium aluminate is added to adjust pH value to more than 12, fluorine ion forms cryolite and separated.Adding calcium hydroxide makes sulphur
Acid group forms calcium sulphate solid and is reclaimed, and obtains sulphur, ammonium, fluorine liquid up to standard up to standard.Liquid up to standard can after sand filter, activated carbon micro-filtration
Into pure water system reuse, zero-emission is realized.
To sum up, the present invention is provided tantalum and niobium hydrometallurgy raffinate and the processing method of comprehensive wastewater, by tungsten ion, fluorine
Ion and sulfate ion and valuable metal ions are separately separated, and realize that it is recycled.Wastewater treatment produces substantial amounts of accessory substance,
Reduce the cost of wastewater treatment.Treatment fluid after raffinate recycling mainly contains ammonium ion, is mixed in containing big
The alkaline waste water for measuring the tantalum and niobium hydrometallurgy of ammonium ion is handled together, simple to operate.
Feature of the invention and performance are described in further detail with reference to embodiments.
Embodiment 1
A kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, including：
Raffinate treatment
Go deacidification clear liquid to obtain concentrate through pellicle raffinate, magnesium fluoride is generated to magnesium hydroxide is added in sour clear liquid
Precipitation, separates fluorination magnesium precipitate.It is that 7 formation tungstenics are precipitated to ammonia to its pH value is passed through in concentrate, separates tungstenic and precipitate
First filtrate.Tungstenic precipitation is dissolved in ammoniacal liquor, filtrate evaporative crystallization is taken and is obtained tungstic acid in 873-973K temperature lower calcinations.
Calculate fluorine ion total amount in the first filtrate, it is 3 to weigh sodium ion total amount with the mol ratio of fluorine ion total amount:6 sodium sulphate and aluminium
Total ion concentration is 1 with the mol ratio of fluorine ion total amount:6 aluminum sulfate.To sulphur acid for adjusting pH value to 5 is added in the first filtrate, add
Sodium sulphate and aluminum sulfate form cryolite precipitation, separate cryolite and precipitate to obtain the second filtrate.To being passed through ammonia in the second filtrate
Gas to pH value is that 8.5 formation are aluminium-containing precipitated, and separation is aluminium-containing precipitated to obtain the 3rd filtrate.Calcium hydroxide is refined to being added in the 3rd filtrate
It is 12 calcium sulfate precipitations formed above to pH value, separating calcium sulphate precipitates to obtain treatment fluid.
Alkaline waste water treatment
The alkaline waste water that treatment fluid and tantalum and niobium hydrometallurgy are produced is mixed into obtain mixed liquor.To adding hydroxide in mixed liquor
Sodium is 9.5 to pH, and the ammonia of effusion is reclaimed with ammonia recycling device, and separation of solid and liquid takes filtrate.Filtrate adds aluminium after deammoniation tower
Sour sodium is 12 formation cryolite precipitations to pH, and separation cryolite precipitation back end hydrogenation calcium oxide forms simultaneously separating calcium sulphate and sinks
Form sediment, remaining liq enters pure water system through sand filter, activated carbon micro-filtration successively.
Embodiment 2
A kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, including：
Raffinate treatment
Raffinate is removed into sour clear liquid through pellicle and obtains concentrate, magnesium fluoride is generated to magnesium hydroxide is added in sour clear liquid
Precipitation, separates fluorination magnesium precipitate.It is that 7.5 formation tungstenics are precipitated to ammonia to its pH value is passed through in concentrate, separates tungstenic precipitation
Obtain the first filtrate.Tungstenic precipitation is dissolved in ammoniacal liquor, filtrate evaporative crystallization is taken and is obtained three oxidations in 873-973K temperature lower calcinations
Tungsten.Calculate fluorine ion total amount in the first filtrate, it is 3.6 to weigh sodium ion total amount with the mol ratio of fluorine ion total amount:6 sodium sulphate
And aluminium ion total amount and the mol ratio of fluorine ion total amount are 1.2:6 aluminum sulfate.Add sulphur acid for adjusting pH value extremely in the first filtrate
6, add sodium sulphate and aluminum sulfate to form cryolite precipitation, separate cryolite and precipitate to obtain the second filtrate.To in the second filtrate
It is that 9.5 formation are aluminium-containing precipitated to be passed through ammonia to pH value, and separation is aluminium-containing precipitated to obtain the 3rd filtrate.Hydrogen is refined to being added in the 3rd filtrate
Calcium oxide to pH value is 12 calcium sulfate precipitations formed above, and separating calcium sulphate precipitates to obtain treatment fluid.
Alkaline waste water treatment
The alkaline waste water that treatment fluid and tantalum and niobium hydrometallurgy are produced is mixed into obtain mixed liquor.To adding hydroxide in mixed liquor
Sodium is 10.5 to pH, and the ammonia of effusion is reclaimed with ammonia recycling device, and separation of solid and liquid takes filtrate.Filtrate adds aluminium after deammoniation tower
Sour sodium is 12.5 formation cryolite precipitations to pH, and separation cryolite precipitation back end hydrogenation calcium oxide forms simultaneously separating calcium sulphate and sinks
Form sediment, remaining liq enters pure water system through sand filter, activated carbon micro-filtration successively.
Embodiment 3
A kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, including：
Raffinate treatment
Raffinate is removed into sour clear liquid through pellicle and obtains concentrate, magnesium fluoride is generated to magnesium hydroxide is added in sour clear liquid
Precipitation, separates fluorination magnesium precipitate.It is that 7.3 formation tungstenics are precipitated to ammonia to its pH value is passed through in concentrate, separates tungstenic precipitation
Obtain the first filtrate.Tungstenic precipitation is dissolved in ammoniacal liquor, filtrate evaporative crystallization is taken and is obtained three oxidations in 873-973K temperature lower calcinations
Tungsten.Calculate fluorine ion total amount in the first filtrate, it is 3.3 to weigh sodium ion total amount with the mol ratio of fluorine ion total amount:6 sodium sulphate
And aluminium ion total amount and the mol ratio of fluorine ion total amount are 1.1:6 aluminum sulfate.Add sulphur acid for adjusting pH value extremely in the first filtrate
5.5, add sodium sulphate and aluminum sulfate to form cryolite precipitation, separate cryolite and precipitate to obtain the second filtrate.To the second filtrate
In to be passed through ammonia to pH value be 9 to form aluminium-containing precipitated, separate aluminium-containing precipitated the 3rd filtrate.Hydrogen is refined to being added in the 3rd filtrate
Calcium oxide to pH value is 12 calcium sulfate precipitations formed above, and separating calcium sulphate precipitates to obtain treatment fluid.
Alkaline waste water treatment
The alkaline waste water that treatment fluid and tantalum and niobium hydrometallurgy are produced is mixed into obtain mixed liquor.To adding hydroxide in mixed liquor
Sodium is 10 to pH, and the ammonia of effusion is reclaimed with ammonia recycling device, and separation of solid and liquid takes filtrate.Filtrate adds aluminic acid after deammoniation tower
Sodium is 12 formation cryolite precipitations to pH, separates cryolite precipitation back end hydrogenation calcium oxide and forms simultaneously separating calcium sulphate precipitation,
Remaining liq enters pure water system through sand filter, activated carbon micro-filtration successively.
After tested, the processing method that embodiment of the present invention 1-3 is provided is average every in the operation for carrying out raffinate treatment
21 yuan of ton raffinate grid electricity fee cost, 1294.8 yuan of medicament (refined lime, ammonia, sodium sulphate and aluminum sulfate) cost, other fees
150.91 yuan of (steam, cost of labor), adds up to 1466.71 yuan.Average raffinate per ton reclaims cryolite 255kg, unit price 7
Unit/kg；Thick tungstic acid 2.5kg, 120 yuan/kg of unit price, add up to recovery product value 2085.Process raffinate warp per ton
Ji benefit is 2085-1466.71=618.29 units.
In sum, the tantalum and niobium hydrometallurgy raffinate and the processing method of comprehensive wastewater of the embodiment of the present invention, will extract
Take the tungsten ion in raffinate, fluorine ion etc. and sequentially form precipitate and separate, be easy to be circulated valuable material comprehensive utilization, process
Low cost.Ion is separated by the form for precipitating, treatment is thorough.And raffinate reclaimed after treatment fluid be mixed in containing
In the alkaline waste water of a large amount of ammonium ions, without individually being post-processed to treatment fluid, technique is saved, it is simple to operate.
Embodiments described above is a part of embodiment of the invention, rather than whole embodiments.Reality of the invention
The detailed description for applying example is not intended to limit the scope of claimed invention, but is merely representative of selected implementation of the invention
Example.Based on the embodiment in the present invention, what those of ordinary skill in the art were obtained under the premise of creative work is not made
His embodiment every other, belongs to the scope of protection of the invention.
Claims (10)
1. a kind of processing method of tantalum and niobium hydrometallurgy raffinate, it is characterised in that including：Raffinate is grasped as follows
Make：
PH value is adjusted with ammonia or ammoniacal liquor and form precipitation to 7-7.5, separate for the first time；
With sulphur acid for adjusting pH value to 5-6, precipitation, second separation are formed in the presence of aluminium salt and sodium salt；
PH value is adjusted to more than 12 with calcium hydroxide, and precipitation and separation obtains treatment fluid.
2. processing method according to claim 1, it is characterised in that before adjusting pH value with ammonia or ammoniacal liquor, to described
Raffinate is diffused dialysis treatment and removes the clear liquid that deacidifies.
3. processing method according to claim 1, it is characterised in that the sodium salt is sodium sulphate, the aluminium salt is sulfuric acid
Aluminium.
4. processing method according to claim 3, it is characterised in that the inventory of sodium ion, the aluminium in the sodium salt
The ratio between amount of material of fluorine ion is 3-3.6 in aluminum ions inventory and the raffinate in salt:1-1.2:6.
5. processing method according to claim 4, it is characterised in that the inventory of sodium ion, the aluminium in the sodium salt
The ratio between amount of material of fluorine ion is 3.3 in aluminum ions inventory and the raffinate in salt:1.1:6.
6. processing method according to claim 4, it is characterised in that adjusted after second separates and with calcium hydroxide
Before pH value, pH value to 8.5-9.5, precipitation and separation is adjusted with ammonia or ammoniacal liquor.
7. processing method according to claim 1, it is characterised in that collect precipitation isolated for the first time, use ammoniacal liquor
To be calcined after filtrate crystallisation after dissolving.
8. processing method according to claim 7, it is characterised in that calcining is carried out under the conditions of 873-973K.
9. a kind of processing method of tantalum and niobium hydrometallurgy comprehensive wastewater, it is characterised in that described in usage right requirement any one of 1-8
Disposal methods described in raffinate, then the alkaline waste water that the treatment fluid that will be obtained is produced with tantalum and niobium hydrometallurgy mixes
Close.
10. processing method according to claim 9, it is characterised in that the mixed liquor to mixing is adjusted with NaOH
PH value to 9.5-10.5 reclaim ammonia.
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| CN112310500A (en) * | 2019-07-31 | 2021-02-02 | 中国科学院过程工程研究所 | Method for separating aluminum element from waste lithium iron phosphate material |
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Application publication date: 20170620 |