CN112678933A - Recycling method of magnesium ammonium phosphate - Google Patents
Recycling method of magnesium ammonium phosphate Download PDFInfo
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- CN112678933A CN112678933A CN202011467283.2A CN202011467283A CN112678933A CN 112678933 A CN112678933 A CN 112678933A CN 202011467283 A CN202011467283 A CN 202011467283A CN 112678933 A CN112678933 A CN 112678933A
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- magnesium
- ammonium phosphate
- phosphate
- magnesium ammonium
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- 229910052567 struvite Inorganic materials 0.000 title claims abstract description 53
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000004064 recycling Methods 0.000 title claims abstract description 16
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 57
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 54
- 239000002002 slurry Substances 0.000 claims abstract description 28
- 238000005292 vacuum distillation Methods 0.000 claims abstract description 26
- 239000002351 wastewater Substances 0.000 claims abstract description 23
- 238000004140 cleaning Methods 0.000 claims abstract description 22
- 239000000203 mixture Substances 0.000 claims abstract description 20
- 239000007787 solid Substances 0.000 claims abstract description 19
- YJGHGAPHHZGFMF-UHFFFAOYSA-K magnesium;sodium;phosphate Chemical compound [Na+].[Mg+2].[O-]P([O-])([O-])=O YJGHGAPHHZGFMF-UHFFFAOYSA-K 0.000 claims abstract description 18
- MHJAJDCZWVHCPF-UHFFFAOYSA-L dimagnesium phosphate Chemical compound [Mg+2].OP([O-])([O-])=O MHJAJDCZWVHCPF-UHFFFAOYSA-L 0.000 claims abstract description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 16
- 238000009833 condensation Methods 0.000 claims abstract description 16
- 230000005494 condensation Effects 0.000 claims abstract description 16
- 229910000395 dimagnesium phosphate Inorganic materials 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 230000008929 regeneration Effects 0.000 claims abstract description 14
- 238000011069 regeneration method Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 229910001479 sodium magnesium phosphate Inorganic materials 0.000 claims abstract description 12
- 239000003513 alkali Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 238000003756 stirring Methods 0.000 claims abstract description 9
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 9
- 238000004821 distillation Methods 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims abstract description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 239000013043 chemical agent Substances 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 20
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 9
- 125000004122 cyclic group Chemical group 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000000197 pyrolysis Methods 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 3
- 229910019142 PO4 Inorganic materials 0.000 description 2
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000009388 chemical precipitation Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 159000000003 magnesium salts Chemical class 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 229960002261 magnesium phosphate Drugs 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The invention discloses a method for recycling magnesium ammonium phosphate, which comprises the following steps: stirring and cleaning magnesium ammonium phosphate generated by treating ammonia nitrogen wastewater with water, and filtering and separating; mixing the washed magnesium ammonium phosphate with a sodium hydroxide solution to obtain first slurry, placing the first slurry in a distillation device connected with a condensation absorption device, and carrying out vacuum distillation treatment to obtain second slurry and condensation absorption liquid; and carrying out liquid-solid separation on the second slurry after vacuum distillation to obtain a mixture of magnesium hydrogen phosphate and sodium magnesium phosphate and concentrated alkali liquor. And recycling the mixture of magnesium hydrogen phosphate and sodium magnesium phosphate for ammonia nitrogen treatment, and recycling the concentrated alkali liquor for magnesium ammonium phosphate regeneration. The method is simple and easy to implement, is suitable for treating ammonia nitrogen wastewater with different concentrations in different industries, realizes the recycling of chemical agents, is beneficial to reducing the treatment cost, and has positive significance for wastewater treatment.
Description
Technical Field
The invention relates to a magnesium ammonium phosphate recycling method, belongs to the field of environmental protection, and particularly relates to magnesium ammonium phosphate recycling for treating ammonia nitrogen wastewater by a chemical precipitation method.
Background
The magnesium ammonium phosphate precipitation method is characterized in that magnesium ions and phosphate ions are added into ammonia nitrogen wastewater to generate insoluble magnesium ammonium phosphate precipitate (MAP) with ammonia nitrogen, so that the aim of removing ammonia nitrogen is fulfilled. The process has the advantages of simple operation, strong capability of treating high-concentration ammonia nitrogen wastewater and the like, but the treatment cost is difficult to accept due to the high price of soluble magnesium salt and phosphate; even if the product magnesium ammonium phosphate can be sold and used as a slow release fertilizer, the market is limited, so that the popularization and application of a magnesium ammonium phosphate precipitation method in ammonia nitrogen wastewater treatment are limited. Therefore, the method has positive significance for carrying out regeneration treatment and recycling on magnesium ammonium phosphate and treating ammonia nitrogen wastewater at low cost.
Kenichi et al, Japan, in Ammonia Removal from Wate waters, disclose a process in which a mixture of alkali and salt is added to magnesium ammonium phosphate precipitate, a small amount of water is added, and then the mixture is heated at 70 to 80 ℃ with stirring for 4 hours to release Ammonia gas, to obtain a pyrolysis product.
In the environmental engineering journal of 2013, No. 7 pyrolysis behavior of cyclic utilization of struvite for treating high ammonia-nitrogen wastewater, the optimal pyrolysis conditions of struvite are as follows: NH (NH)4+The molar ratio is 1:1, the temperature is 90 ℃, the heating time is 4h, the denitrification rate reaches 95 percent, and the ammonia nitrogen removal rate is over 80 percent after 6 times of recycling.
The existing alkali-added pyrolysis method has the defects of long pyrolysis time, high medicament consumption, easy corrosion of equipment and the like although the denitrification rate is high.
Disclosure of Invention
The invention aims to provide a rapid and effective magnesium ammonium phosphate regeneration treatment method, which can reduce the treatment cost of ammonia nitrogen wastewater while realizing recycling.
The technical scheme adopted by the invention is as follows:
a method for recycling magnesium ammonium phosphate comprises the following steps:
(1) stirring and cleaning: and (3) stirring and cleaning magnesium ammonium phosphate generated by treating the ammonia nitrogen wastewater with water, filtering and separating when COD (chemical oxygen demand) in the cleaning solution is lower than 200mg/L, and finishing cleaning. The purpose of stirring and cleaning is to reduce organic matters carried in the magnesium ammonium phosphate so as to avoid the accumulation of the organic matters during the subsequent circulation of concentrated alkali liquor, influence the vacuum distillation and increase the COD in the condensed water.
(2) Vacuum distillation: mixing the washed magnesium ammonium phosphate with a sodium hydroxide solution to obtain first slurry, placing the first slurry in a distillation device connected with a condensation absorption device, and carrying out vacuum distillation treatment to obtain second slurry and condensation absorption liquid; wherein the concentration of the sodium hydroxide is 3-10%, the liquid-solid volume ratio of the sodium hydroxide solution to the magnesium ammonium phosphate is (5-8): 1, the vacuum degree is 15-30 kPa, the vacuum distillation temperature is 60-80 ℃, and the vacuum distillation time is 30-50 min.
(3) Liquid-solid separation: and carrying out liquid-solid separation on the second slurry after vacuum distillation to obtain a mixture of magnesium hydrogen phosphate and sodium magnesium phosphate and concentrated alkali liquor.
By adopting the technical scheme, the magnesium ammonium phosphate generated by treating the ammonia nitrogen wastewater by the chemical precipitation method in the step 1) can be regenerated only by simple washing treatment, and ammonia nitrogen, organic matters and the like carried in the magnesium ammonium phosphate can be removed by stirring and cleaning. In the step 2) of the scheme, boiling evaporation can be realized at a lower temperature through vacuum distillation under an alkaline condition, bubbles generated by boiling can promote rapid overflow of ammonia, the alkali concentration is gradually increased along with water evaporation, and the ammonia volatilization speed is accelerated, so that the thermodynamic and kinetic conditions of the magnesium ammonium phosphate denitrification reaction are enhanced. The main reaction equation in the process is as follows:
NH4MgPO4·6H2O→MgHPO4·3H2O+NH3+3H2O
NH4MgPO4·6H2O+NaOH→MgNaPO4·3H2O+NH3+4H2O
magnesium hydrogen phosphate MgHPO formed4·3H2O, sodium magnesium phosphate MgNaPO4·3H2The O mixture can be directly applied to the treatment of ammonia nitrogen wastewater, and the effect is similar to the effect of adding phosphate and magnesium salt to remove ammonia nitrogen.
Further, the mixture of magnesium hydrogen phosphate and sodium magnesium phosphate obtained by the liquid-solid separation in the step (3) can be directly applied to ammonia nitrogen wastewater treatment without drying treatment; the obtained concentrated alkali liquor can be diluted and used for denitrification regeneration of magnesium ammonium phosphate again.
The invention has the following advantages:
1. compared with the prior art, under the vacuum condition, the regeneration time of magnesium ammonium phosphate is short, and the denitrification rate is high;
2. compared with the prior art, the magnesium ammonium phosphate can realize denitrification regeneration at a lower temperature;
3. compared with the prior art, the added alkali can be recycled, and the regeneration cost is saved.
4. Compared with the prior art, the magnesium ammonium phosphate can realize infinite regeneration and recycling, the produced mixture of the magnesium ammonium phosphate and the sodium magnesium phosphate can be directly used for treating ammonia nitrogen wastewater, and the ammonia nitrogen removal effect is stabilized to be more than 80%.
Drawings
FIG. 1 is a flow chart of a process for recycling magnesium ammonium phosphate.
Detailed Description
The present invention will be described in further detail with reference to examples.
Example 1:
(1) 25g of magnesium ammonium phosphate (the water content is 60 percent and the nitrogen content is 5.71 percent) generated by ammonia nitrogen wastewater treatment is taken, stirred and cleaned by water, filtered and separated when COD in a cleaning solution is lower than 200mg/L, and the cleaning is finished.
(2) Mixing the cleaned magnesium ammonium phosphate with a 3% NaOH solution, and controlling the liquid-solid ratio (volume ratio) of the sodium hydroxide solution to the magnesium ammonium phosphate to be 5: 1, obtaining a first slurry; and (3) putting the first slurry into a distillation device connected with a condensation absorption device for vacuum distillation, controlling the vacuum degree to be 15kPa, the vacuum distillation temperature to be 60 ℃, and the vacuum distillation time to be 40min, thus obtaining second slurry and condensation absorption liquid.
(3) And taking out the second slurry for liquid-solid separation, taking out a mixture of magnesium hydrogen phosphate and magnesium sodium phosphate, and detecting that the nitrogen content is 0.51 percent and the denitrification rate reaches 91.1 percent.
(4) The mixture of magnesium hydrogen phosphate and sodium magnesium phosphate is used for treating 500ml of ammonia nitrogen wastewater containing 200mg/L ammonia nitrogen, and the ammonia nitrogen removal rate reaches 95.9%.
(5) After 5 times of cyclic regeneration, 500ml of ammonia nitrogen wastewater containing 200mg/L ammonia nitrogen is treated, and the ammonia nitrogen removal rate can still reach 93.6%.
Example 2:
(1) 25g of magnesium ammonium phosphate (the water content is 60 percent and the nitrogen content is 5.71 percent) generated by ammonia nitrogen wastewater treatment is taken, stirred and cleaned by water, filtered and separated when COD in a cleaning solution is lower than 200mg/L, and the cleaning is finished.
(2) Mixing the cleaned magnesium ammonium phosphate with 10% NaOH, wherein the liquid-solid ratio (volume ratio) of the sodium hydroxide solution to the magnesium ammonium phosphate is 6: and 1, putting the obtained first slurry into a distillation device connected with a condensation absorption device for vacuum distillation, controlling the vacuum degree to be 15kPa, the temperature to be 70 ℃, and the vacuum distillation time to be 40min to obtain second slurry and condensation absorption liquid.
(3) And taking out the second slurry for liquid-solid separation, taking out a mixture of magnesium hydrogen phosphate and magnesium sodium phosphate, and detecting that the nitrogen content is 0.41 percent and the denitrification rate reaches 92.8 percent.
(4) The mixture of magnesium hydrogen phosphate and sodium magnesium phosphate is used for treating 500ml of ammonia nitrogen wastewater containing 200mg/L ammonia nitrogen, and the ammonia nitrogen removal rate reaches 96.2%.
(5) After 8 times of cyclic regeneration, 500ml of ammonia nitrogen wastewater containing 200mg/L is treated, and the ammonia nitrogen removal rate can still reach 92.5 percent.
Example 3:
(1) taking 25g of magnesium ammonium phosphate (the water content is 60% and the nitrogen content is 5.71%) generated by ammonia nitrogen wastewater treatment, stirring and cleaning with water, filtering and separating when COD in a cleaning solution is lower than 200mg/L, and finishing cleaning;
(2) mixing the cleaned magnesium ammonium phosphate with 7% NaOH, wherein the liquid-solid ratio (volume ratio) of the sodium hydroxide solution to the magnesium ammonium phosphate is 7: and 1, putting the obtained first slurry into a distillation device connected with a condensation absorption device for vacuum distillation, controlling the vacuum degree to be 20kPa, the temperature to be 80 ℃, and the vacuum distillation time to be 30min to obtain second slurry and condensation absorption liquid.
(3) And taking out the second slurry for liquid-solid separation, taking out a mixture of magnesium hydrogen phosphate and magnesium sodium phosphate, and detecting that the nitrogen content is 0.50% and the denitrification rate reaches 91.2%.
(4) The mixture of magnesium hydrogen phosphate and sodium magnesium phosphate is used for treating 500m ammonia nitrogen wastewater with ammonia nitrogen concentration of 400mg/L, and the ammonia nitrogen removal rate reaches 96.0%.
(5) After 10 times of cyclic regeneration, 500ml of ammonia nitrogen wastewater containing 400mg/L ammonia nitrogen is treated, and the ammonia nitrogen removal rate can still reach 91.8%.
Example 4:
(1) 25g of magnesium ammonium phosphate (the water content is 60 percent and the nitrogen content is 5.71 percent) generated by ammonia nitrogen wastewater treatment is taken, stirred and cleaned by water, filtered and separated when COD in a cleaning solution is lower than 200mg/L, and the cleaning is finished.
(2) Mixing the cleaned magnesium ammonium phosphate with 5% NaOH, wherein the liquid-solid ratio (volume ratio) of the sodium hydroxide solution to the magnesium ammonium phosphate is 8: 1, putting the obtained first slurry into a distillation device connected with a condensation absorption device for vacuum distillation, controlling the vacuum degree to be 15kPa, the temperature to be 60 ℃ and the vacuum distillation time to be 40min, and obtaining second slurry and condensation absorption liquid;
(3) and taking out the second slurry for liquid-solid separation, taking out a mixture of magnesium hydrogen phosphate and magnesium sodium phosphate, and detecting that the nitrogen content is 0.48% and the denitrification rate reaches 91.6%.
(4) The mixture of magnesium hydrogen phosphate and sodium magnesium phosphate is used for treating 500ml of ammonia nitrogen wastewater containing 1000mg/L ammonia nitrogen, and the ammonia nitrogen removal rate reaches 93.5%.
(5) After 15 times of cyclic regeneration, 500ml of ammonia nitrogen wastewater containing 1000mg/L ammonia nitrogen is treated, and the ammonia nitrogen removal rate can still reach 90.9%.
Example 5: (1) 75g of magnesium ammonium phosphate (the water content is 60 percent and the nitrogen content is 5.71 percent) generated by ammonia nitrogen wastewater treatment is taken, stirred and cleaned by water, filtered and separated when COD in the cleaning solution is lower than 200mg/L, and the cleaning is finished. (2) Mixing the cleaned magnesium ammonium phosphate with 3% NaOH, wherein the liquid-solid ratio (volume ratio) of the sodium hydroxide solution to the magnesium ammonium phosphate is 5: 1, putting the obtained first slurry into a distillation device connected with a condensation absorption device for vacuum distillation, controlling the vacuum degree to be 30kPa, the temperature to be 80 ℃ and the vacuum distillation time to be 50min, and obtaining second slurry and condensation absorption liquid;
(3) and taking out the second slurry for liquid-solid separation, taking out a mixture of magnesium hydrogen phosphate and magnesium sodium phosphate, and detecting that the nitrogen content is 0.55% and the denitrification rate reaches 90.4%.
(4) The mixture of magnesium hydrogen phosphate and sodium magnesium phosphate is used for treating 500ml of ammonia nitrogen wastewater containing 3000mg/L ammonia nitrogen, and the ammonia nitrogen removal rate reaches 87.9%.
(5) After 20 times of cyclic regeneration, 500ml of ammonia nitrogen wastewater containing 3000mg/L ammonia nitrogen is treated, and the ammonia nitrogen removal rate can still reach 84.5%.
The process conditions, costs and effects of examples 1-5 are shown in table 1.
Table 1 process conditions and costs and effects of examples 1-5
Claims (2)
1. The recycling method of magnesium ammonium phosphate is characterized by comprising the following steps:
(1) stirring and cleaning: stirring and cleaning magnesium ammonium phosphate generated by treating ammonia nitrogen wastewater with water, filtering and separating when COD (chemical oxygen demand) in cleaning liquid is lower than 200mg/L, and finishing cleaning;
(2) vacuum distillation: mixing magnesium ammonium phosphate cleaned in the step (1) with a sodium hydroxide solution to obtain first slurry, placing the first slurry in a distillation device connected with a condensation absorption device, and carrying out vacuum distillation treatment to obtain second slurry and a condensation absorption liquid; the mass concentration of the sodium hydroxide solution is 3-10%, and the liquid-solid volume ratio of the sodium hydroxide solution to the magnesium ammonium phosphate is (5-8): 1; the control conditions of the vacuum distillation are as follows: the vacuum degree is 15-30 kPa, the vacuum distillation temperature is 60-80 ℃, and the vacuum distillation time is 30-50 min;
(3) liquid-solid separation: and carrying out liquid-solid separation on the second slurry after vacuum distillation to obtain a mixture of magnesium hydrogen phosphate and sodium magnesium phosphate and concentrated alkali liquor.
2. The recycling method of magnesium ammonium phosphate according to claim 1, wherein the mixture of magnesium ammonium phosphate and magnesium sodium phosphate obtained by the liquid-solid separation in the step (3) can be directly applied to ammonia nitrogen wastewater treatment; the obtained concentrated alkali liquor can be diluted and used for denitrification regeneration of magnesium ammonium phosphate.
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| CN202011467283.2A CN112678933A (en) | 2020-12-11 | 2020-12-11 | Recycling method of magnesium ammonium phosphate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113943871A (en) * | 2021-10-21 | 2022-01-18 | 崇义章源钨业股份有限公司 | Method for treating magnesium ammonium phosphate slag containing tungsten |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0490396A1 (en) * | 1990-12-14 | 1992-06-17 | DEUTSCHE NALCO-CHEMIE GmbH | Process for recovery of ammonia from process and waste waters |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
| CN102674523A (en) * | 2012-05-24 | 2012-09-19 | 南京大学 | Method for recycling ammonia and nitrogen in waste watery by aid of chemicrystallization |
| CN106586992A (en) * | 2016-12-10 | 2017-04-26 | 包头稀土研究院 | Comprehensive fluorine and phosphorous recovery technology for liquid caustic soda decomposition of mixed rare earth concentrate |
-
2020
- 2020-12-11 CN CN202011467283.2A patent/CN112678933A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0490396A1 (en) * | 1990-12-14 | 1992-06-17 | DEUTSCHE NALCO-CHEMIE GmbH | Process for recovery of ammonia from process and waste waters |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
| CN102674523A (en) * | 2012-05-24 | 2012-09-19 | 南京大学 | Method for recycling ammonia and nitrogen in waste watery by aid of chemicrystallization |
| CN106586992A (en) * | 2016-12-10 | 2017-04-26 | 包头稀土研究院 | Comprehensive fluorine and phosphorous recovery technology for liquid caustic soda decomposition of mixed rare earth concentrate |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113943871A (en) * | 2021-10-21 | 2022-01-18 | 崇义章源钨业股份有限公司 | Method for treating magnesium ammonium phosphate slag containing tungsten |
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