CN103523800B - Method for recovering excess sodium hydroxide in tungsten smelting crude sodium tungstate solution - Google Patents
Method for recovering excess sodium hydroxide in tungsten smelting crude sodium tungstate solution Download PDFInfo
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Abstract
The invention discloses a method for recovering excess sodium hydroxide in a tungsten smelting crude sodium tungstate solution. The method comprises the steps of mixing a tungsten ore raw material and water according to the volume ratio of 10: 3, then adding into a ball mill for ball milling to obtain tungsten ore slurry, adding a sodium hydroxide solution into the tungsten ore slurry to perform alkali autoclaving to obtain alkali autoclaved slurry, and performing pressure filtration on the alkali autoclaved slurry twice so as to obtain a crude sodium tungstate solution; pumping the crude sodium tungstate solution into a feeding and preheating device; enabling sodium tungstate crystal slurry obtained by separation after the well preheated crude sodium tungstate solution sequentially passes through a three-effect evaporation unit, a one-effect evaporation unit and a two-effect evaporation unit for evaporation and crystallization to enter a plate frame for pressure filtration so as to obtain a concentrated odium hydroxide solution and sodium tungstate crystals. The method disclosed by the invention has the advantages of high degree of automation, convenience in operation and capabilities of greatly reducing energy consumption, reducing later-stage wastewater neutralization control burden, reducing labor cost, reducing labor intensity and being easy to implement, and is in line with the national policies of reducing cost, increasing efficiency, saving energy and reducing emission.
Description
Technical field
The present invention relates to Tungsten smelting technical field, be mainly concerned with the recovery method of excess hydrogen sodium oxide in a kind of Tungsten smelting coarse sodium tungstate.
Background technology
Along with the continuous exploitation of tungsten ore resource, the especially high-grade wolframite reserves of tungsten concentrate are fewer and feweri, and white tungsten fine ore and the higher chats of foreign matter content become the main source of Tungsten smelting raw material in the future.In prior art, the smelting of white tungsten fine ore and chats generally adopts high basic pressure digestion technology, throws 2.8 ~ 4 times that alkali number is generally theoretical amount, superfluous NaOH and WO in the coarse sodium tungstate obtained after the press filtration of basic pressure digestion slurry
3mass ratio reach 0.7 ~ 1.2, even higher, if do not reclaimed, not only disadvantageous effect is brought to subsequent handling, and finally also will consume after sulfuric acid neutralizes it and could discharge.No matter therefore from reducing starting material unit consumption, reducing production cost or have the necessity reclaiming superfluous NaOH Tungsten smelting coarse sodium tungstate from the angle of environment protection, energy-saving and emission-reduction.
The recovery method of superfluous NaOH mainly condensing crystal method in current Tungsten smelting coarse sodium tungstate, the single-effect evaporation crystallizing pan steam indirect heating adopting band to stir reaches the object of condensing crystal.Condensing crystal ratio juris is that the changes in solubility of sodium wolframate under different naoh concentrations is large, along with the rising of naoh concentration, the solubleness of sodium wolframate is successively decreased, so constantly concentrating along with sodium hydroxide solution, it is more and more that sodium wolframate crystallization just occurs, thus both separated.Facts have proved, there is the problems such as energy consumption is high, efficiency is low, running cost is high, level of automation is low, environmental protection pressure is large in the recovery adopting this original evaporation technique to carry out superfluous NaOH in Tungsten smelting coarse sodium tungstate.
Chinese patent CN102963911A discloses a kind of method reclaiming remaining alkali from the sodium tungstate solution Tungsten smelting, still mixed liquor is out boiled by the filtrate after pressure filter solid-liquor separation from pressure, with being pumped into triple effect evaporation crystallizer, first enter in first preheating tube and carry out preheating, then an effect evaporative crystallizer is entered, the secondary steam that one effect evaporation concentration produces is as the thermal source of two effect evaporation concentration, and the sodium wolframate crystal that two effect evaporative crystallizers are separated out send plate-and-frame filter press to carry out solid-liquid separation; Concentrated solution continues to enter in Three-effect concentration device, and the sodium wolframate crystal that triple effect evaporation crystallizer is separated out carries out solid-liquid separation through plate-and-frame filter press; The sodium wolframate crystal that two effect evaporative crystallizers and triple effect evaporation crystallizer are separated out together enters plate-and-frame filter press and carries out solid-liquid separation; Filtrate enters storage tank and joins alkali in order to return pressure boiling procedure, and filter residue is discharged in dissolving tank.The weak point of the method is: one is the system of three-effect downstream evaporator technique adopted, than three-effect counter flow or triple effect mixed flow process energy consumption larger, such as basic industry process is containing NaOH 125 ~ 135g/L, the solution of NaCl190 ~ 210g/L produces NaOH concentration when being the liquid caustic soda of 42 ~ 50%, adopt system of three-effect downstream evaporator then NaOH consumption steam per ton 3.5 ~ 3.8t, adopt three-effect counter flow/triple effect mixed flow evaporation then NaOH consumption steam per ton 2.6 ~ 2.8t, energy consumption significantly reduces than system of three-effect downstream evaporator; Two is that two effect evaporative crystallization sections have existed the precipitation of sodium wolframate crystal, though be furnished with brilliant mouth, along with the rising of mixed liquid concentration, viscosity strengthens gradually, still easily causes the fouling of heating tube side, causes plugging to occur.
The inventive method adopts triple effect mixed flow method of evaporating to reclaim excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate, it is considerably less that sodium wolframate crystallization in evaporative process is imitated in triple effect evaporation and, there will not be plugging phenomenon, not only reduce sodium hydroxide cost recovery, energy-conserving and environment-protective, and improve sodium wolframate percent crystallization in massecuite.
Summary of the invention
The object of the invention is to solve above-mentioned prior art Problems existing, and a kind of technique provided simple, be easy to realize, the recovery method of superfluous NaOH in energy consumption is low, wide adaptability, level of automation are high Tungsten smelting coarse sodium tungstate.
The present invention is the recovery method disclosing excess hydrogen sodium oxide in a kind of Tungsten smelting coarse sodium tungstate for the technical scheme solved the problems of the technologies described above, and it is characterized in that, comprises the following steps:
Step one, tungsten ore raw material and water are mixed add in ball mill ball milling obtain tungsten ore starch by volume at 10: 3, sodium hydroxide solution is added in described tungsten ore slurry, described sodium hydroxide solution addition is that in described sodium hydroxide solution, sodium hydrate content is 1.0 ~ 1.4 times of tungstic oxide content in described tungsten ore raw material, entered during band stirs by the described tungsten ore stock pump adding described sodium hydroxide solution afterwards to press in reactor and carry out basic pressure digestion acquisition basic pressure digestion slurry, described basic pressure digestion slurry obtains coarse sodium tungstate after twice press filtration;
Step 2, described coarse sodium tungstate is sent into through fresh feed pump in the reinforced primary heater unit of triple effect evaporation crystallizer, when described coarse sodium tungstate preheating temperature reaches the boiling temperature of triple effect evaporation modular heater, described coarse sodium tungstate pumps into the evaporation unit of triple effect evaporation unit, gas-liquid separation is carried out through triple effect fractional crystallization device after evaporation concentration, separating obtained residue vapor enters condensing works, separating obtained once concentration liquid enters the evaporation unit of an effect evaporation element, carries out gas-liquid separation after evaporation concentration through an effect fractional crystallization device;
Step 3, described once concentration liquid is after a described effect fractional crystallization device carries out gas-liquid separation, separating obtained primary steam enters the evaporation unit of two effect evaporation elements as heating source, separating obtained secondary concentration liquid enters the evaporation unit of two effect evaporation elements, carries out gas-liquid separation after condensing crystal through two effect fractional crystallization devices;
Step 4, described secondary concentration liquid is through two effect fractional crystallization devices, separating obtained secondary steam enters the evaporation unit of described triple effect evaporation unit as heat source, separating obtained sodium wolframate magma enters filter press, filtrate is that concentrated sodium hydroxide solution returns ammonium paratungstate production flow process, and filter residue is enter solution preparation operation before Tungsten smelting ion-exchange after the press filtration of sodium wolframate dissolution of crystals.
Preferably, described in described step one, during basic pressure digestion, liquid-solid ratio is 1 ~ 1.2: 1.
Preferably, be 80 ~ 150g/L and tungstic oxide mass concentration be 150 ~ 180g/L containing sodium hydroxide mass concentration in coarse sodium tungstate described in described step one.
Preferably, the cold in-water temperature of described condensing works is 32 ~ 35 DEG C, and leaving water temperature(LWT) is 38 ~ 40 DEG C.
Preferably, the water of condensation obtained by described condensing works returns described ammonium paratungstate production flow process.
Preferably, the temperature in of the raw steam of evaporation unit of an effect evaporation element described in described step 3 is 155 DEG C, and vapor pressure is 0.3 ~ 0.5MPa.
Preferably, described in described step 4, secondary concentration liquid mass percent concentration is less than 42%.
The amount of adding sodium hydroxide in described basic pressure digestion process in described tungsten ore slurry is generally, 2.8 ~ 4.0 times of theoretical amount alkali, and described theoretical alkali charge is one ton of tungstic oxide (WO
3) consume 0.345t sodium hydroxide, such as: one ton of tungsten ore raw material is containing 0.5 ton of WO
3, one ton of tungsten ore consumes sodium hydroxide:
1t×0.5t×0.345×(2.8～4.0)＝(0.5～0.7)t。
The invention has the beneficial effects as follows that the inventive method adopts triple effect mixed flow evaporation technology, the low-temperature evaporation realizing solution under vacuum conditions concentrates, and concentrated effect is good, and energy consumption is low, and environmental protection pressure is little, and level of automation is high; The inventive method is by the strict mass percent concentration controlling the sodium wolframate of triple effect evaporation unit and the separating obtained concentrated solution of an effect evaporation element, effectively prevent sodium wolframate crystallization from occurring, thus effectively stop the fouling of well heater tube side, good effect of heat exchange, consume the energy low; The inventive method concentrates crystallization sodium wolframate at two effect evaporation elements, makes sodium wolframate organic efficiency high; After excess hydrogen sodium oxide in coarse sodium tungstate is reclaimed, liquid processing cost after follow-up Tungsten smelting ion-exchange can be reduced, reduce use the sulfuric acid amount of adjust ph in Tungsten smelting waste water dis posal process, greatly reduction resource expend the expenditure with cost.In a word, the inventive method level of automation is high, easy to operate, than the energy-conservation and low the present invention of labour intensity of interval absorption method than traditional single-effect evaporation crystallization process, can significantly reduce energy consumption, alleviate later stage waste water neutralize improvement burden, reduce cost of labor, reduce labour intensity, level of automation is high, easy to operate, easily realize, meet the policy of national cost efficiency, energy-saving and emission-reduction.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail, can implement according to this with reference to specification sheets word to make those skilled in the art.
Embodiment 1
As shown in Figure 1, in Tungsten smelting coarse sodium tungstate, the recovery method of excess hydrogen sodium oxide is:
Step one, tungsten ore raw material and water are mixed add in ball mill ball milling obtain tungsten ore starch by volume at 10: 3, sodium hydroxide solution is added in described tungsten ore slurry, described sodium hydroxide solution addition is that in described sodium hydroxide solution, sodium hydrate content is 1.0 times of tungstic oxide content in described tungsten ore raw material, afterwards the described tungsten ore stock pump adding described sodium hydroxide solution is entered during band stirs to press in reactor and carry out basic pressure digestion acquisition basic pressure digestion slurry, during basic pressure digestion, liquid-solid ratio is generally 1 ~ 1.2: 1, described basic pressure digestion slurry obtains coarse sodium tungstate after twice press filtration,
Wherein, 80g/L and 150g/L is respectively containing sodium hydroxide and tungstic oxide mass concentration in described coarse sodium tungstate;
Step 2, described coarse sodium tungstate is sent into through fresh feed pump in the reinforced primary heater unit of triple effect evaporation crystallizer, when described coarse sodium tungstate preheating temperature reaches the boiling temperature of triple effect evaporation modular heater, described coarse sodium tungstate is pumped into the evaporation unit of described triple effect evaporation unit, gas-liquid separation is carried out through triple effect fractional crystallization device after evaporation concentration, separating obtained residue vapor enters condensing works, separating obtained once concentration liquid enters the evaporation unit of an effect evaporation element, carries out gas-liquid separation after evaporation concentration through an effect fractional crystallization device;
Wherein, described condensing works cold in-water temperature is 32 DEG C ~ 35 DEG C, and leaving water temperature(LWT) is 38 DEG C ~ 40 DEG C, and in described once concentration liquid, sodium wolframate mass percent concentration is 27.2%
Step 3, described once concentration liquid is after a described effect fractional crystallization device carries out gas-liquid separation, separating obtained primary steam enters the evaporation unit of two effect evaporation elements as heating source, separating obtained secondary concentration liquid enters the evaporation unit of two effect evaporation elements, carries out gas-liquid separation after condensing crystal through two effect fractional crystallization devices;
Wherein, the temperature in of the raw steam of evaporation unit of a described effect evaporation element is 155 DEG C, and vapor pressure is 0.5MPa, and in described secondary concentration liquid, sodium wolframate mass percent concentration is 40.5%;
Step 4, described secondary concentration liquid is after described two effect fractional crystallization devices carry out gas-liquid separation, separating obtained secondary steam enters the evaporation unit of described triple effect evaporation unit as heating source, it is that concentrated sodium hydroxide solution returns ammonium paratungstate production flow process that separating obtained sodium wolframate magma enters filter press gained filtrate, and gained filter residue is that sodium wolframate crystal enters solution preparation operation before Tungsten smelting ion-exchange.
Wherein, in described filtrate, the concentration of sodium hydroxide is 308g/L, WO
3concentration be 36g/L, WO
3percent crystallization in massecuite be 94.0%, the rate of recovery of sodium hydroxide is 96.3%.
Embodiment 2
As shown in Figure 1, in Tungsten smelting coarse sodium tungstate, the recovery method of excess hydrogen sodium oxide is:
Step one, tungsten ore raw material and water are mixed add in ball mill ball milling obtain tungsten ore starch by volume at 10: 3, sodium hydroxide solution is added in described tungsten ore slurry, described sodium hydroxide solution addition is that in described sodium hydroxide solution, sodium hydrate content is 1.2 times of tungstic oxide content in described tungsten ore raw material, afterwards the described tungsten ore stock pump adding described sodium hydroxide solution is entered during band stirs to press in reactor and carry out basic pressure digestion acquisition basic pressure digestion slurry, during basic pressure digestion, liquid-solid ratio is generally 1 ~ 1.2: 1, described basic pressure digestion slurry obtains coarse sodium tungstate after twice press filtration,
Wherein, 100g/L and 165g/L is respectively containing sodium hydroxide and tungstic oxide mass concentration in described coarse sodium tungstate;
Step 2, described coarse sodium tungstate is sent into through fresh feed pump in the reinforced primary heater unit of triple effect evaporation crystallizer, when described coarse sodium tungstate preheating temperature reaches the boiling temperature of triple effect evaporation modular heater, described coarse sodium tungstate is pumped into the evaporation unit of described triple effect evaporation unit, gas-liquid separation is carried out through triple effect fractional crystallization device after evaporation concentration, separating obtained residue vapor enters condensing works, separating obtained once concentration liquid enters the evaporation unit of an effect evaporation element, carries out gas-liquid separation after evaporation concentration through an effect fractional crystallization device;
Wherein, described condensing works cold in-water temperature is 32 DEG C ~ 35 DEG C, and leaving water temperature(LWT) is 38 DEG C ~ 40 DEG C, and in described once concentration liquid, sodium wolframate mass percent concentration is 28.0%
Step 3, described once concentration liquid is after a described effect fractional crystallization device carries out gas-liquid separation, separating obtained primary steam enters the evaporation unit of two effect evaporation elements as heating source, separating obtained secondary concentration liquid enters the evaporation unit of two effect evaporation elements, carries out gas-liquid separation after condensing crystal through two effect fractional crystallization devices;
Wherein, the temperature in of the raw steam of evaporation unit of a described effect evaporation element is 155 DEG C, and vapor pressure is 0.5MPa, and in described secondary concentration liquid, sodium wolframate mass percent concentration is 41.3%;
Step 4, described secondary concentration liquid is after described two effect fractional crystallization devices carry out gas-liquid separation, separating obtained secondary steam enters the evaporation unit of described triple effect evaporation unit as heating source, it is that concentrated sodium hydroxide solution returns ammonium paratungstate production flow process that separating obtained sodium wolframate magma enters filter press gained filtrate, and gained filter residue is that sodium wolframate crystal enters solution preparation operation before Tungsten smelting ion-exchange.
Wherein, in described filtrate, the concentration of sodium hydroxide is 353g/L, WO
3concentration be 24g/L, WO
3percent crystallization in massecuite be 96.0%, the rate of recovery of sodium hydroxide is 97.1%.
Embodiment 3
As shown in Figure 1, in Tungsten smelting coarse sodium tungstate, the recovery method of excess hydrogen sodium oxide is:
Step one, tungsten ore raw material and water are mixed add in ball mill ball milling obtain tungsten ore starch by volume at 10: 3, sodium hydroxide solution is added in described tungsten ore slurry, described sodium hydroxide solution addition is that in described sodium hydroxide solution, sodium hydrate content is 1.4 times of tungstic oxide content in described tungsten ore raw material, afterwards the described tungsten ore stock pump adding described sodium hydroxide solution is entered during band stirs to press in reactor and carry out basic pressure digestion acquisition basic pressure digestion slurry, during basic pressure digestion, liquid-solid ratio is generally 1 ~ 1.2: 1, described basic pressure digestion slurry obtains coarse sodium tungstate after twice press filtration,
Wherein, 150g/L and 180g/L is respectively containing sodium hydroxide and tungstic oxide mass concentration in described coarse sodium tungstate;
Step 2, described coarse sodium tungstate is sent into through fresh feed pump in the reinforced primary heater unit of triple effect evaporation crystallizer, when described coarse sodium tungstate preheating temperature reaches the boiling temperature of triple effect evaporation modular heater, described coarse sodium tungstate is pumped into the evaporation unit of described triple effect evaporation unit, gas-liquid separation is carried out through triple effect fractional crystallization device after evaporation concentration, separating obtained residue vapor enters condensing works, separating obtained once concentration liquid enters the evaporation unit of an effect evaporation element, carries out gas-liquid separation after evaporation concentration through an effect fractional crystallization device;
Wherein, described condensing works cold in-water temperature is 32 DEG C ~ 35 DEG C, and leaving water temperature(LWT) is 38 DEG C ~ 40 DEG C, and in described once concentration liquid, sodium wolframate mass percent concentration is 28.7%
Step 3, described once concentration liquid is after a described effect fractional crystallization device carries out gas-liquid separation, separating obtained primary steam enters the evaporation unit of two effect evaporation elements as heating source, separating obtained secondary concentration liquid enters the evaporation unit of two effect evaporation elements, carries out gas-liquid separation after condensing crystal through two effect fractional crystallization devices;
Wherein, the temperature in of the raw steam of evaporation unit of a described effect evaporation element is 155 DEG C, and vapor pressure is 0.5MPa, and in described secondary concentration liquid, sodium wolframate mass percent concentration is 41.7%;
Step 4, described secondary concentration liquid is after described two effect fractional crystallization devices carry out gas-liquid separation, separating obtained secondary steam enters the evaporation unit of described triple effect evaporation unit as heating source, it is that concentrated sodium hydroxide solution returns ammonium paratungstate production flow process that separating obtained sodium wolframate magma enters filter press gained filtrate, and gained filter residue is that sodium wolframate crystal enters solution preparation operation before Tungsten smelting ion-exchange.
Wherein, in described filtrate, the concentration of sodium hydroxide is 373g/L, WO
3concentration be 17g/L, WO
3percent crystallization in massecuite be 96.3%, the rate of recovery of sodium hydroxide is 97.4%.
Although embodiment of the present invention are open as above, but it is not restricted to listed in specification sheets and embodiment utilization, it can be applied to various applicable the field of the invention completely, for those skilled in the art, can easily realize other amendment, therefore do not deviating under the universal that claim and equivalency range limit, the present invention is not limited to specific details and illustrates here and the legend described.
Claims (8)
1. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate, is characterized in that, comprise the following steps:
Step one, tungsten ore raw material and water are mixed add in ball mill ball milling obtain tungsten ore starch by volume at 10: 3, sodium hydroxide solution is added in described tungsten ore slurry, described sodium hydroxide solution addition is that in described sodium hydroxide solution, sodium hydrate content is 1.0 ~ 1.4 times of tungstic oxide content in described tungsten ore raw material, entered during band stirs by the described tungsten ore stock pump adding described sodium hydroxide solution afterwards to press in reactor and carry out basic pressure digestion acquisition basic pressure digestion slurry, described basic pressure digestion slurry obtains coarse sodium tungstate after twice press filtration;
Step 2, described coarse sodium tungstate is sent into through fresh feed pump in the reinforced primary heater unit of triple effect evaporation crystallizer, when described coarse sodium tungstate preheating temperature reaches the boiling temperature of triple effect evaporation modular heater, described coarse sodium tungstate is pumped into the evaporation unit of described triple effect crystalline element, gas-liquid separation is carried out through triple effect fractional crystallization device after evaporation concentration, separating obtained residue vapor enters condensing works, separating obtained once concentration liquid enters the evaporation unit of an effect evaporation element, carries out gas-liquid separation after evaporation concentration through an effect fractional crystallization device;
Step 3, described once concentration liquid is after an effect fractional crystallization device of a described effect evaporation element carries out gas-liquid separation, separating obtained primary steam enters the evaporation unit of two effect evaporation elements as heating source, separating obtained secondary concentration liquid enters the evaporation unit of two effect evaporation elements, carries out gas-liquid separation after condensing crystal through two effect fractional crystallization devices;
Step 4, described secondary concentration liquid is after two effect fractional crystallization devices of described two effect evaporation elements carry out gas-liquid separation, separating obtained secondary steam enters the evaporation unit of described triple effect evaporation unit as heating source, it is that concentrated sodium hydroxide solution returns ammonium paratungstate production flow process that separating obtained sodium wolframate magma enters filter press gained filtrate, and gained filter residue is that sodium wolframate crystal enters solution preparation operation before Tungsten smelting ion-exchange.
2. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, described in described step one, during basic pressure digestion, liquid-solid ratio is 1 ~ 1.2: 1.
3. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, in coarse sodium tungstate described in described step one, be respectively 80 ~ 150g/L and 150 ~ 180g/L containing sodium hydroxide and tungstic oxide mass concentration.
4. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, the cold in-water temperature of described condensing works is 32 DEG C ~ 35 DEG C, and leaving water temperature(LWT) is 38 DEG C ~ 40 DEG C.
5. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, the water of condensation obtained by described condensing works returns described ammonium paratungstate production flow process.
6. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, the temperature in of the raw steam of evaporation unit of an effect evaporation element described in described step 3 is 155 DEG C, and vapor pressure is 0.3 ~ 0.5MPa.
7. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, described in described step 4, secondary concentration liquid mass percent concentration is less than 42%.
8. the recovery method of excess hydrogen sodium oxide in Tungsten smelting coarse sodium tungstate as claimed in claim 1, it is characterized in that, ammonium paratungstate production flow process described in described step 4 comprises basic pressure digestion operation and ball milling operation.
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| CN104556231A (en) * | 2014-12-27 | 2015-04-29 | 山东天维膜技术有限公司 | Preparation method of sodium tungstate solution and method for recovering alkaline in preparation process |
| CN104789772B (en) * | 2015-04-06 | 2017-01-04 | 桂林理工大学 | The method that the leaching of a kind of scheelite alkali is energy-saving and cost-reducing |
| CN109824064B (en) * | 2019-03-25 | 2020-02-07 | 中南大学 | Method for recovering sodium carbonate from sodium tungstate leaching solution |
| CN110551892A (en) * | 2019-10-17 | 2019-12-10 | 中国恩菲工程技术有限公司 | mineral separation device containing tungsten-tin concentrate |
| CN110760703B (en) * | 2019-11-20 | 2021-09-03 | 中国有色集团（广西）平桂飞碟股份有限公司 | Method for recovering tungsten from waste APT powder |
| CN115353148A (en) * | 2022-08-31 | 2022-11-18 | 赣州有色冶金研究所有限公司 | Method for recovering sodium hydroxide from sodium tungstate alkali cooking liquor |
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| JP5100104B2 (en) * | 2006-12-19 | 2012-12-19 | 日本錬水株式会社 | Method for producing ammonium tungstate aqueous solution |
| CN102963911A (en) * | 2012-11-14 | 2013-03-13 | 中湘钨业股份有限公司 | Method of recycling residual alkali from sodium tungstate solution in tungsten smelting |
| CN103103359B (en) * | 2012-11-23 | 2014-05-14 | 陈泉兴 | Method for regenerating APT (ammonium paratungstate) by use of APT waste low-grade tungsten slag |
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