CN114524540A - Reutilization method of N263 alkaline extraction raffinate - Google Patents
Reutilization method of N263 alkaline extraction raffinate Download PDFInfo
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- CN114524540A CN114524540A CN202210141885.1A CN202210141885A CN114524540A CN 114524540 A CN114524540 A CN 114524540A CN 202210141885 A CN202210141885 A CN 202210141885A CN 114524540 A CN114524540 A CN 114524540A
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- 238000000605 extraction Methods 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000005406 washing Methods 0.000 claims abstract description 57
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000000292 calcium oxide Substances 0.000 claims abstract description 20
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000001914 filtration Methods 0.000 claims abstract description 19
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 19
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 19
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 16
- 239000011347 resin Substances 0.000 claims abstract description 12
- 229920005989 resin Polymers 0.000 claims abstract description 12
- 239000000706 filtrate Substances 0.000 claims abstract description 11
- 239000011550 stock solution Substances 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 230000001276 controlling effect Effects 0.000 claims description 13
- 239000002002 slurry Substances 0.000 claims description 10
- 238000003795 desorption Methods 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 6
- 238000005070 sampling Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- 125000002924 primary amino group Chemical class [H]N([H])* 0.000 claims description 3
- 239000000243 solution Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 1
- 230000001568 sexual effect Effects 0.000 claims 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 abstract description 7
- 239000010937 tungsten Substances 0.000 abstract description 7
- 229910052750 molybdenum Inorganic materials 0.000 abstract description 6
- 229910052721 tungsten Inorganic materials 0.000 abstract description 6
- 239000011733 molybdenum Substances 0.000 abstract description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 abstract description 3
- 238000001179 sorption measurement Methods 0.000 abstract description 3
- 239000002893 slag Substances 0.000 abstract 2
- 238000010438 heat treatment Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- 238000003723 Smelting Methods 0.000 description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- MGRWKWACZDFZJT-UHFFFAOYSA-N molybdenum tungsten Chemical compound [Mo].[W] MGRWKWACZDFZJT-UHFFFAOYSA-N 0.000 description 2
- 239000012074 organic phase Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 229910001182 Mo alloy Inorganic materials 0.000 description 1
- 229910001080 W alloy Inorganic materials 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/34—Obtaining molybdenum
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/36—Obtaining tungsten
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
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- Water Supply & Treatment (AREA)
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Abstract
The invention relates to a method for secondary utilization of N263 alkaline extraction raffinate, which comprises magnesium oxide/calcium oxide/active carbon purification-Filtering, washing, secondary utilization and the like. The method comprises purifying under heating with calcium oxide to remove excessive HCO in raffinate3、CO3P and entrained organic matters are filtered and washed, purified slag and filtrate are separated, the purified slag is collected and treated, the filtrate is secondarily utilized and is used for desorbing macroporous resin D314/D318 saturated in adsorption of high-molybdenum feed liquid, or is used for adjusting the pH value of an N263 alkaline extraction section or is used for adjusting the pH value of an N1923 extraction separation tungsten and molybdenum extraction stock solution, and finally the efficient secondary utilization of the N263 alkaline extraction raffinate is completed, so that the treatment cost is reduced.
Description
Technical Field
The invention relates to the technical field of tungsten and molybdenum smelting, in particular to a secondary utilization method of N263 alkaline extraction raffinate.
Background
Tungsten and molybdenum belong to rare metals, and have excellent physical and chemical properties, so that the tungsten and molybdenum alloy is widely applied to various fields. With the gradual increase of the national requirements for environmental protection, the subsequent wastewater treatment cost is remarkably increased due to the large amount of wastewater generated in the operation process of the traditional tungsten smelting process (ion exchange process), and the long-term development of the tungsten smelting industry is influenced. In order to overcome the problems of large waste water amount and high treatment cost of the traditional ion exchange process for tungsten smelting, students develop a new smelting process which comprises a sulfuric-phosphoric mixed acid leaching-acid extraction process and an N263 alkaline extraction process, so that the industrial application is realized, and the water-saving effect is obvious. In the N263 alkaline extraction process, because of the loaded organic phase clarification section in the extraction process, washing water is required to be added to wash the extraction stock solution (washing Na) carried by the loaded organic phase+) The volume of the raffinate tends to increase gradually, which causes the phenomenon of the raffinate occupying the tank, and is not beneficial to operation, and in addition, as the recycling frequency of the raffinate increases, CO in the raffinate3 2-And impurity elements such as P can be enriched, which seriously influences the extraction effect.
The invention aims at the problems that the raffinate is gradually increased in the running process of the N263 alkaline extraction, the raffinate occupies a groove, and CO is contained in the raffinate3 2-And the enrichment of impurity elements such as P and the like to influence the subsequent extraction effect, develops a method for secondary utilization of N263 alkaline extraction raffinate, and the method utilizes magnesium oxide/calcium oxide/active carbonPurifying, filtering, washing, secondary utilization and the like to finish the treatment of CO in the N263 alkaline extraction raffinate3 2-And impurity elements such as P and the like are purified and removed, secondary utilization is realized, the problem that the raffinate occupies more slots is solved, and the method is a method for efficiently and secondarily utilizing the N263 alkaline extraction raffinate.
Disclosure of Invention
The invention aims to provide a method for recycling N263 alkaline extraction raffinate.
The technical problem of the invention is mainly solved by the following technical scheme:
a method for recycling N263 alkaline extraction raffinate comprises the following steps:
(1) purifying magnesium oxide, calcium oxide and active carbon: adding magnesium oxide, calcium oxide and active carbon into the N263 alkaline extraction raffinate, and stirring, wherein the adding amount is controlled to be 1-5g/L of magnesium oxide, 20-100g/L of calcium oxide and 1-5g/L of active carbon, after the reaction is finished, sampling and filtering to ensure that CO 32-is less than 20g/L, the concentration of NaOH is more than 70g/L and P is less than 0.2g/L in the feed liquid;
(2) filtering and washing: filtering the slurry obtained in the step (1), collecting the purified filtrate, and then washing with hot water, wherein the washed hot water is washed in a circulating secondary washing mode, and the volume of the washing water is controlled to be 0.5-1 times of the volume of the slurry each time;
(3) secondary utilization: and (3) carrying out secondary utilization on the filtered filtrate after purification:
firstly, desorbing the saturated resin adsorbed by macroporous resin D318/D314, wherein the volume of a desorbent is 1.5-2.0 times of the volume of the resin, the flow of the desorbent is controlled to be 0.8-1.2 times of the volume of the resin, and performing circulating desorption, wherein a desorption solution is returned after being boiled at high temperature and is used as an extraction stock solution of N263 alkaline extraction;
regulating the pH value of the N263 alkaline extraction section, and controlling the pH value end point to be more than or equal to 13;
thirdly, adjusting the pH value of the primary amine N1923 alkalescent extraction stock solution, adjusting the pH value, circulating for 30-60min, and controlling the end point pH value to be 7.5-8.0.
As a preferable scheme, when magnesium oxide, calcium oxide and active carbon are added into the N263 alkaline extraction raffinate and stirred, wherein the stirring speed is 60-90r/min, the reaction time is 60-90min, and the reaction temperature is 80-90 ℃.
Preferably, the temperature of the hot water for washing the hot water in the step (2) is controlled to be 50-80 ℃, wherein the hot water is from the boiler condensed water.
As a preferable scheme, the specific operation mode of circulating the secondary washing in the step (2) is as follows: the first washing, collecting and treating after washing with 0.5-1 times volume of hot water, then carrying out the second washing, continuing washing with 0.5-1 times volume of hot water, and collecting the washing water as the washing water for the first washing in the next period.
The invention has the beneficial effects that: the method for removing CO from the N263 alkaline extraction raffinate is completed by the methods of purifying, filtering, washing, secondary utilization and the like of magnesium oxide, calcium oxide and active carbon3 2-And P and other impurity elements, the problem that the raffinate is increased to occupy the tank is solved, the efficient reutilization of the increased raffinate is realized, and the treatment cost is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The technical scheme of the invention is further specifically described by the following embodiments and the accompanying drawings.
Example 1
A secondary utilization method of N263 alkaline extraction raffinate, in this example, the N263 alkaline extraction raffinate comes from Ganzhou tungsten molybdenum smeltery, and the sampling and detecting result is WO35.13g/L, Mo 0.56g/L, P0.65 g/L, total C (sodium carbonate or sodium bicarbonate) 142.61 g/L.
(1) Purifying magnesium oxide, calcium oxide and active carbon: will be 10m3Pumping N263 alkaline extraction raffinate into 15m3Adding magnesium oxide, calcium oxide and active carbon into a volume stirring tank, controlling the adding amount to be 5g/L of magnesium oxide, 80g/L of calcium oxide and 1-5g/L of active carbon, wherein the stirring speed is 60r/min, the reaction time is 60min, the reaction temperature is 90 ℃, completing the reaction, sampling and filtering, and adding the magnesium oxide, the calcium oxide and the active carbon into the volume stirring tankCO32-15.33g/L, NaOH concentration 101.24g/L and P0.12 g/L, and then entering the next link.
(2) Filtering and washing: filtering the slurry obtained in the step (1), collecting the purified filtrate, then washing with hot water, controlling the temperature of the hot water to be 50-80 ℃ (the hot water comes from boiler condensate), washing the hot water in a circulating secondary washing mode, controlling the volume of the washing water to be 0.5-1 time of the volume of the slurry every time, and specifically, carrying out the first washing, collecting and processing the slurry after the washing with 1 time of the volume of the hot water, then carrying out the second washing, continuously washing with 1 time of the volume of the hot water, collecting the washing water (serving as the washing water for the first washing in the next period), completing the filtering and washing, and entering the next link.
(3) Secondary utilization: filtering the filtrate after purification to obtain 20m3And secondary utilization is carried out, namely, the macroporous resin D314 is used for desorbing the saturated adsorption resin, and the volume of the resin is 10m3Adsorption of WO32231.58kg, adsorbing Mo 214.42kg, and purifying to obtain filtrate with volume of 17m3The desorption flow rate was controlled to 10m3H, carrying out circulating desorption, wherein the volume of the desorption solution is 17m3The detection result is WO3 127.12g/L，Mo 11.89g/L，WO3And the desorption rates of Mo and Mo are 96.84% and 94.27% respectively, and the Mo is returned to be used as the extraction stock solution of N263 alkaline extraction after being boiled at high temperature.
Example 2
A secondary utilization method of N263 alkaline extraction raffinate, in this example, the N263 alkaline extraction raffinate comes from Ganzhou tungsten molybdenum smeltery, and the sampling and detecting result is WO34.03g/L, Mo 0.37g/L, P0.35 g/L, total C (sodium carbonate or sodium bicarbonate) 123.91 g/L.
(1) Purifying magnesium oxide, calcium oxide and active carbon: will be 10m3Pumping N263 alkaline extraction raffinate into 15m3Adding magnesium oxide, calcium oxide and active carbon into a volume stirring tank, controlling the adding amount to be 5g/L of magnesium oxide, 100g/L of calcium oxide and 1-5g/L of active carbon, stirring at a speed of 60r/min, reacting for 60min, controlling the reaction temperature to be 90 ℃, completing the reaction, sampling and filtering, and adding CO in the feed liquid3 2-10.54g/L, NaOH concentration 95.26g/L, P0.1And 0g/L, entering the next link.
(2) Filtering and washing: filtering the slurry obtained in the step (1), collecting the purified filtrate, then washing with hot water, controlling the temperature of the hot water to be 50-80 ℃ (the hot water comes from boiler condensate), washing the hot water in a circulating secondary washing mode, controlling the volume of the washing water to be 0.5-1 time of the volume of the slurry every time, and specifically, carrying out the first washing, collecting and processing the slurry after the washing with 1 time of the volume of the hot water, then carrying out the second washing, continuously washing with 1 time of the volume of the hot water, collecting the washing water (serving as the washing water for the first washing in the next period), completing the filtering and washing, and entering the next link.
(3) Secondary utilization: filtering the filtrate after purification to obtain 20m3The secondary utilization is carried out for the second time,
the method is used for adjusting the pH value of the N263 alkaline extraction section, and the pH value end point is adjusted to be controlled to be more than or equal to 13 of the pH value of raffinate effluent, so that the operation is normal; the method is used for adjusting the pH value of primary amine N1923 alkalescent extraction stock solution, adjusting the pH value, circulating for 30-60min, controlling the end point pH value to be 7.5-8.0, and operating normally.
The method of the invention uses magnesium oxide/calcium oxide/active carbon for purification, and completes the essential transformation of the raffinate from a sodium carbonate system to a sodium hydroxide system, and the sodium carbonate has no desorption function.
The present invention has been described in detail, but the above description is only a preferred embodiment of the present invention, and is not to be construed as limiting the scope of the present invention. All equivalent changes and modifications made within the scope of the present invention shall fall within the scope of the present invention.
Claims (4)
1. A method for recycling N263 alkaline extraction raffinate is characterized by comprising the following steps:
(1) purifying magnesium oxide, calcium oxide and active carbon: at N263 baseAdding magnesium oxide, calcium oxide and active carbon into the sexual extraction raffinate, stirring, controlling the adding amount to be 1-5g/L of magnesium oxide, 20-100g/L of calcium oxide and 1-5g/L of active carbon, sampling and filtering after the reaction is finished, and enabling CO in the feed liquid to be in the form of liquid3 2-Less than 20g/L, the concentration of NaOH is more than 70g/L, and P is less than 0.2 g/L;
(2) filtering and washing: filtering the slurry obtained in the step (1), collecting the purified filtrate, and then washing with hot water, wherein the washed hot water is washed in a circulating secondary washing mode, and the volume of the washing water is controlled to be 0.5-1 times of the volume of the slurry each time;
(3) secondary utilization: and (3) carrying out secondary utilization on the filtered filtrate after purification:
firstly, desorbing the saturated resin adsorbed by macroporous resin D318/D314, wherein the volume of a desorbent is 1.5-2.0 times of the volume of the resin, the flow of the desorbent is controlled to be 0.8-1.2 times of the volume of the resin, and performing circulating desorption, wherein a desorption solution is returned after being boiled at high temperature and is used as an extraction stock solution of N263 alkaline extraction;
regulating the pH value of the N263 alkaline extraction section, and controlling the pH value end point to be more than or equal to 13;
thirdly, adjusting the pH value of the primary amine N1923 alkalescent extraction stock solution, adjusting the pH value, circulating for 30-60min, and controlling the end point pH value to be 7.5-8.0.
2. The method as claimed in claim 1, wherein magnesium oxide, calcium oxide and activated carbon are added to the N263 alkaline raffinate, and the mixture is stirred at a stirring speed of 60-90r/min for 60-90min at a reaction temperature of 80-90 ℃.
3. The method for recycling N263 alkaline extraction raffinate of claim 1, wherein the temperature of the hot water for washing the hot water in the step (2) is controlled to be 50-80 ℃, wherein the hot water is derived from boiler condensed water.
4. The method for recycling N263 alkaline extraction raffinate of claim 1, wherein the operation mode of circulating the secondary washing in the step (2) is as follows: the first washing, collecting and treating after washing with 0.5-1 times volume of hot water, then carrying out the second washing, continuing washing with 0.5-1 times volume of hot water, and collecting the washing water as the washing water for the first washing in the next period.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502715A (en) * | 2011-11-09 | 2012-06-20 | 广东光华科技股份有限公司 | Method for reclaiming reagent-grade anhydrous sodium sulfate from basic nickel carbonate production waste liquor |
| CN102887534A (en) * | 2012-11-07 | 2013-01-23 | 广东光华科技股份有限公司 | Method for recovering reagent level anhydrous sodium sulfate from raffinate obtained in process of extracting nickel from nickel sulfate solution |
| WO2018028543A1 (en) * | 2016-08-08 | 2018-02-15 | 有研稀土新材料股份有限公司 | Method for extraction, enrichment and recovery of rare earths from low-concentration rare earth solution |
| CN111139356A (en) * | 2020-01-19 | 2020-05-12 | 意定(上海)信息科技有限公司 | Method for extracting lithium from lithium-containing low-magnesium brine |
-
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- 2022-02-16 CN CN202210141885.1A patent/CN114524540A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502715A (en) * | 2011-11-09 | 2012-06-20 | 广东光华科技股份有限公司 | Method for reclaiming reagent-grade anhydrous sodium sulfate from basic nickel carbonate production waste liquor |
| CN102887534A (en) * | 2012-11-07 | 2013-01-23 | 广东光华科技股份有限公司 | Method for recovering reagent level anhydrous sodium sulfate from raffinate obtained in process of extracting nickel from nickel sulfate solution |
| WO2018028543A1 (en) * | 2016-08-08 | 2018-02-15 | 有研稀土新材料股份有限公司 | Method for extraction, enrichment and recovery of rare earths from low-concentration rare earth solution |
| CN111139356A (en) * | 2020-01-19 | 2020-05-12 | 意定(上海)信息科技有限公司 | Method for extracting lithium from lithium-containing low-magnesium brine |
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