CN101723527B - recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal - Google Patents
recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal Download PDFInfo
- Publication number
- CN101723527B CN101723527B CN 200910112778 CN200910112778A CN101723527B CN 101723527 B CN101723527 B CN 101723527B CN 200910112778 CN200910112778 CN 200910112778 CN 200910112778 A CN200910112778 A CN 200910112778A CN 101723527 B CN101723527 B CN 101723527B
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- acid
- waste water
- add
- value
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
- Removal Of Specific Substances (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses hydrochloric acid waste liquid mesoxalic acid produced by mining rare-earth metal and a recycling method of hydrochloric acid. The method comprises the processing of hydrochloric acid waste water and the recycling of oxalate, wherein the processing of hydrochloric acid waste water comprises the steps of: firstly, pumping hydrochloric acid waste water into a reaction kettle, adding amino compound till the pH value of the solution is neutral, adding barium chloride solid to stir, filtering and separating out oxalate solid; secondly, removing the obtained filtration in a reaction kettle, adding acid solution, stirring and filtering to obtain the amino compound salt precipitation; finally, passing the filtration through anion exchange resin to obtain the processed hydrochloric acid solution for cyclic utilization; and the recycling of oxalate comprises the steps of: splitting the separated oxalate with hydrochloric acid, then stirring to separate the oxalate solid with high purity through the anion exchange resin. The invention adopts the feature of components in the hydrochloric acid and the principle of controlling waste by waste, thereby completely processing residue of oxalate and metal ion in the hydrochloric acid solution and enabling the processed hydrochloric acid to be recycled continuously.
Description
Technical field
The relevant a kind of method for treating waste liquid of the present invention is meant a kind of hydrochloride waste mesoxalic acid of rare earth metal exploitation generation and the recovery method of hydrochloric acid especially.
Background technology
To rare earth metal (as: terbium sesquioxide, europium sesquioxide, dysprosium oxide, cerium lanthanum oxide, Praseodymium trioxide neodymium) in the recovery process, contains more oxalic acid and metal ions such as calcium, iron in the hydrochloride waste of generation, if it is not recycled, then cause environmental pollution easily, and increase the cost of enterprise.
At present the processing mode in this field generally is to adopt the calcium oxide precipitation, promptly utilizes calcium oxide that hydrochloric acid is neutralized, and filters then, makes the pH value of the waste water after the processing reach emission request; Though this technology can make the pH value of waste water reach emission request, has increased the consuming cost of hydrochloric acid and calcium oxide, and can't make the oxalic acid in the waste water be able to recycling.
Summary of the invention
The purpose of this invention is to provide the hydrochloride waste mesoxalic acid that the exploitation of a kind of rare earth metal produces and the recovery method of hydrochloric acid, can effectively handle the residual of hydrochloride waste mesoxalic acid and metal ion, make the hydrochloric acid soln after the processing continue recycle.
For achieving the above object, solution of the present invention is:
The hydrochloride waste mesoxalic acid that a kind of rare earth metal exploitation produces and the recovery method of hydrochloric acid, it comprises the steps:
1), the processing of hydrochloric acid waste water
At first with in the hydrochloric acid waste water suction reactor, add amino-complex, the pH value that makes solution adds the bariumchloride solid again and stirs for neutral, filters, and isolates the oxalate solid; Secondly the filtrate that obtains is moved in the reactor, add acid solution, stir after-filtration, thereby obtain amino-complex salt precipitation; At last this filtrate is passed through anionite-exchange resin, promptly get the hydrochloric acid soln recycle after handling;
2), the recovery of oxalic acid
Isolated oxalate solid is carried out acidolysis with hydrochloric acid, stir then, by anionite-exchange resin, isolate highly purified oxalic acid solid again.
Hydrochloric acid waste water in the described step 1), amino-complex and bariumchloride solid mass ratio are 1: (0.08-0.25): (0.02-0.06).
Add amino-complex in the described step 1) and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, stirred 1 to 4 hour; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 2 to 3 hours.
Described step 2) the pH value of acidolysis control solution is 0.5 in, and stirring at room is 2 hours then.
Described step 1) is handled the hydrochloric acid waste water that the europium sesquioxide exploitation produces, and hydrochloric acid waste water, N propyl aniline and bariumchloride solid mass ratio are 1: 0.1: 0.03; Add N propyl aniline and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 2 hours; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
Described step 1) is handled the hydrochloric acid waste water that the dysprosium oxide exploitation produces, and hydrochloric acid waste water, dianisidine and bariumchloride solid mass ratio are 1: 0.15: 0.05; Add dianisidine and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 3 hours; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
Described step 1) is handled the hydrochloric acid waste water that the terbium sesquioxide exploitation produces, and hydrochloric acid waste water, N-bromotrifluoromethane phthalic imidine and bariumchloride solid mass ratio are 1: 0.08: 0.02; Add N-bromotrifluoromethane phthalic imidine and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 1 hour; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
Described step 1) is handled the hydrochloric acid waste water that the cerium lanthanum oxide exploitation produces, and hydrochloric acid waste water, N-acetonitrile phthalic imidine and bariumchloride solid mass ratio are 1: 0.2: 0.06; Add N-acetonitrile phthalic imidine and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 4 hours; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
Described step 1) is handled the hydrochloric acid waste water that the exploitation of Praseodymium trioxide neodymium produces, and hydrochloric acid waste water, 2-methyl-5 N-methyl-p-nitroaniline and bariumchloride solid mass ratio are 1: 0.25: 0.06; Add 2-methyl-5 N-methyl-p-nitroaniline and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 4 hours; And then be about 0.5 with the pH value of acid-conditioning solution, stirred 3 hours.
After adopting such scheme, the present invention makes full use of the characteristics of each component in this hydrochloric acid soln, adopt the principle of the treatment of wastes with processes of wastes against one another, not only handled the residual of hydrochloride waste mesoxalic acid and metal ion more completely, and made the hydrochloric acid soln after the processing can continue recycle.
Embodiment
The processing mode of the hydrochloric acid waste water that produces when (1) the rare earth metal europium sesquioxide is exploited: utilize lift pump with in one ton the hydrochloric acid waste water suction reactor, add 0.1 ton of N propyl aniline then, the pH value that makes solution stirs half an hour for neutral; In reactor, add 0.03 ton of bariumchloride solid again, continue to stir 2 hours, filter, isolate the oxalate solid.Utilize lift pump to move in the reactor again the filtrate that obtains, and then be about 0.5, stir 2 hours after-filtration, obtain N propyl aniline salt solid with the pH value of acid-conditioning solution; Then this filtrate is passed through anionite-exchange resin once more, promptly get the hydrochloric acid soln after handling, this hydrochloric acid soln mesoxalic acid content is lower than 50 mg/litre, and the content of metal ion is lower than 20 mg/litre, and this hydrochloric acid soln can continue recycle.
The recovery technology of oxalic acid: isolated oxalate solid is carried out acidolysis with hydrochloric acid, and the pH value of control solution is about 0.5, and stirring at room is 2 hours then, again by anionite-exchange resin, thereby isolates highly purified oxalic acid solid.
The processing mode of the hydrochloric acid waste water that produces when (2) the rare earth metal dysprosium oxide is exploited: utilize lift pump with in one ton the hydrochloric acid waste water suction reactor, add 0.15 ton of dianisidine then, the pH value that makes solution stirs half an hour for neutral; In reactor, add 0.05 ton of bariumchloride solid again, continue to stir 3 hours, filter, isolate the oxalate solid.Utilize lift pump to move in the reactor again the filtrate that obtains, and then be about 0.5, stir 2 hours after-filtration, obtain dianisidine salt solid with the pH value of acid-conditioning solution; Then this filtrate is passed through anionite-exchange resin once more, promptly get the hydrochloric acid soln after handling, this hydrochloric acid soln mesoxalic acid content is lower than 30 mg/litre, and the content of metal ion is lower than 10 mg/litre, and this hydrochloric acid soln can continue recycle.
The recovery technology of oxalic acid: the recovery method of the hydrochloric acid waste water mesoxalic acid that produces when this technology such as europium sesquioxide exploitation.
The processing mode of the hydrochloric acid waste water that produces when (3) the rare earth metal terbium sesquioxide is exploited: utilize lift pump with in one ton the hydrochloric acid waste water suction reactor, add 0.08 ton of N-bromotrifluoromethane phthalic imidine then, the pH value that makes solution stirs half an hour for neutral; In reactor, add 0.02 ton of bariumchloride solid again, continue to stir 1 hour, filter, isolate the oxalate solid.Utilize lift pump to move in the reactor again the filtrate that obtains, and then be about 0.5, stir 2 hours after-filtration, obtain N-bromotrifluoromethane phthalic imidine salt solid with the pH value of acid-conditioning solution; Then this filtrate is passed through anionite-exchange resin once more, promptly get the hydrochloric acid soln after handling, this hydrochloric acid soln mesoxalic acid content is lower than 40 mg/litre, and the content of metal ion is lower than 15 mg/litre, and this hydrochloric acid soln can continue recycle.
The recovery technology of oxalic acid: the recovery method of the hydrochloric acid waste water mesoxalic acid that produces when this technology such as europium sesquioxide exploitation.
The processing mode of the hydrochloric acid waste water that produces when (4) the rare earth metal cerium lanthanum oxide is exploited: utilize lift pump with in one ton the hydrochloric acid waste water suction reactor, add 0.2 ton of N-acetonitrile phthalic imidine then, the pH value that makes solution stirs half an hour for neutral; In reactor, add 0.06 ton of bariumchloride solid again, continue to stir 4 hours, filter, isolate the oxalate solid.Utilize lift pump to move in the reactor again the filtrate that obtains, and then be about 0.5, stir 2 hours after-filtration, obtain N-acetonitrile phthalic imidine salt solid with the pH value of acid-conditioning solution; Then this filtrate is passed through anionite-exchange resin once more, promptly get the hydrochloric acid soln after handling, this hydrochloric acid soln mesoxalic acid content is lower than 60 mg/litre, and the content of metal ion is lower than 10 mg/litre, and this hydrochloric acid soln can continue recycle.
The recovery technology of oxalic acid: the recovery method of the hydrochloric acid waste water mesoxalic acid that produces when this technology such as europium sesquioxide exploitation.
The processing mode of the hydrochloric acid waste water that produces when (5) rare earth metal Praseodymium trioxide neodymium is exploited: utilize lift pump with in one ton the hydrochloric acid waste water suction reactor, add 0.25 ton of 2-methyl-5 N-methyl-p-nitroaniline then, the pH value that makes solution stirs half an hour for neutral; In reactor, add 0.06 ton of bariumchloride solid again, continue to stir 4 hours, filter, isolate the oxalate solid.Utilize lift pump to move in the reactor again the filtrate that obtains, and then be about 0.5, stir 3 hours after-filtration, obtain 2-methyl-5 oil of mirbane amine salt solid with the pH value of acid-conditioning solution; Then this filtrate is passed through anionite-exchange resin once more, promptly get the hydrochloric acid soln after handling, this hydrochloric acid soln mesoxalic acid content is lower than 30 mg/litre, and the content of metal ion is lower than 10 mg/litre, and this hydrochloric acid soln can continue recycle.
The recovery technology of oxalic acid: the recovery method of the hydrochloric acid waste water mesoxalic acid that produces when this technology such as europium sesquioxide exploitation.
Claims (9)
1. a rare earth metal is exploited the hydrochloride waste mesoxalic acid of generation and the recovery method of hydrochloric acid, and it comprises the steps:
1), the processing of hydrochloric acid waste water
At first with in the hydrochloric acid waste water suction reactor, add amino-complex, the pH value that makes solution adds the bariumchloride solid again and stirs for neutral, filters, and isolates the oxalate solid; Secondly the filtrate that obtains is moved in the reactor, add acid solution, stir after-filtration, thereby obtain amino-complex salt precipitation; At last this filtrate is passed through anionite-exchange resin, promptly get the hydrochloric acid soln recycle after handling;
2), the recovery of oxalic acid
Isolated oxalate solid is carried out acidolysis with hydrochloric acid, stir then, by anionite-exchange resin, isolate highly purified oxalic acid solid again.
2. the hydrochloride waste mesoxalic acid that rare earth metal exploitation as claimed in claim 1 produces and the recovery method of hydrochloric acid, it is characterized in that: the hydrochloric acid waste water in the described step 1), amino-complex and bariumchloride solid mass ratio are 1: (0.08-0.25): (0.02-0.06).
3. the hydrochloride waste mesoxalic acid that rare earth metal exploitation as claimed in claim 1 produces and the recovery method of hydrochloric acid is characterized in that: add amino-complex in the step 1) and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, stirred 1 to 4 hour; And then be 0.5 with the pH value of acid-conditioning solution, stirred 2 to 3 hours.
4. the hydrochloride waste mesoxalic acid that rare earth metal as claimed in claim 1 exploitation produces and the recovery method of hydrochloric acid is characterized in that: step 2) in the pH value of acidolysis control solution be 0.5, stirring at room is 2 hours then.
5. as claim 1, the hydrochloride waste mesoxalic acid of 2 or 3 described rare earth metal exploitation generations and the recovery method of hydrochloric acid, it is characterized in that: step 1) is handled the hydrochloric acid waste water that the europium sesquioxide exploitation produces, and hydrochloric acid waste water, N propyl aniline and bariumchloride solid mass ratio are 1: 0.1: 0.03; Add N propyl aniline and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 2 hours; And then be 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
6. as claim 1, the hydrochloride waste mesoxalic acid of 2 or 3 described rare earth metal exploitation generations and the recovery method of hydrochloric acid, it is characterized in that: step 1) is handled the hydrochloric acid waste water that the dysprosium oxide exploitation produces, and hydrochloric acid waste water, dianisidine and bariumchloride solid mass ratio are 1: 0.15: 0.05; Add dianisidine and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 3 hours; And then be 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
7. as claim 1, the hydrochloride waste mesoxalic acid of 2 or 3 described rare earth metal exploitation generations and the recovery method of hydrochloric acid, it is characterized in that: step 1) is handled the hydrochloric acid waste water that the terbium sesquioxide exploitation produces, and hydrochloric acid waste water, N-bromotrifluoromethane phthalic imidine and bariumchloride solid mass ratio are 1: 0.08: 0.02; Add N-bromotrifluoromethane phthalic imidine and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 1 hour; And then be 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
8. as claim 1, the hydrochloride waste mesoxalic acid of 2 or 3 described rare earth metal exploitation generations and the recovery method of hydrochloric acid, it is characterized in that: step 1) is handled the hydrochloric acid waste water that the cerium lanthanum oxide exploitation produces, and hydrochloric acid waste water, N-acetonitrile phthalic imidine salt and bariumchloride solid mass ratio are 1: 0.2: 0.06; Add N-acetonitrile phthalic imidine salt and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 4 hours; And then be 0.5 with the pH value of acid-conditioning solution, stirred 2 hours.
9. as claim 1, the hydrochloride waste mesoxalic acid of 2 or 3 described rare earth metal exploitation generations and the recovery method of hydrochloric acid, it is characterized in that: described step 1) is handled the hydrochloric acid waste water that the exploitation of Praseodymium trioxide neodymium produces, and hydrochloric acid waste water, 2-methyl-5 N-methyl-p-nitroaniline and bariumchloride solid mass ratio are 1: 0.25: 0.06; Add 2-methyl-5 N-methyl-p-nitroaniline and make the pH value of solution be neutrality, stir half an hour; Add the bariumchloride solid again, need to stir 4 hours; And then be 0.5 with the pH value of acid-conditioning solution, stirred 3 hours.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910112778 CN101723527B (en) | 2009-11-05 | 2009-11-05 | recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910112778 CN101723527B (en) | 2009-11-05 | 2009-11-05 | recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101723527A CN101723527A (en) | 2010-06-09 |
| CN101723527B true CN101723527B (en) | 2011-08-24 |
Family
ID=42445180
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200910112778 Expired - Fee Related CN101723527B (en) | 2009-11-05 | 2009-11-05 | recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101723527B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102976525B (en) * | 2012-12-12 | 2013-11-20 | 南昌大学 | Method for treating and recycling rare earth oxalate precipitation mother solution |
| CN104086398B (en) * | 2014-07-15 | 2015-10-28 | 中南大学 | A kind of method of oxalic acid waste liquid Separation and Recovery oxalic acid |
| CN104357670B (en) * | 2014-11-04 | 2016-05-18 | 江西理工大学 | A kind of method of recycling with slag for comprehensive in rare earth oxalic acid waste water |
| CN109987740A (en) * | 2019-01-29 | 2019-07-09 | 厦门稀土材料研究所 | The method for precipitating calcium and magnesium in industrial wastewater |
-
2009
- 2009-11-05 CN CN 200910112778 patent/CN101723527B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN101723527A (en) | 2010-06-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108642310B (en) | Method for removing aluminum from rare earth feed liquid by complexing precipitation | |
| CN104294063B (en) | The method of low concentration of rare earth solution extraction and recovery rare earth | |
| CN103570161B (en) | A kind of fluoride ion removing method in hamartite rare earth metallurgy | |
| AU2014339746A1 (en) | Deriving high value products from waste red mud | |
| CN106367621B (en) | The method of valuable element is recycled and recycled from low content earth solution and precipitation slag | |
| CN107699715B (en) | The method of extracting and enriching recovering rare earth from low concentration of rare earth solution | |
| CN101723527B (en) | recycling method of oxalic acid and hydrochloric acid from hydrochloric acid waste liquid produced by mining rare-earth metal | |
| CN103288248B (en) | Combined treatment method for rear earth smelting/separating wastewater | |
| CN106367622A (en) | High-efficient and green ion-absorbed-type rear earth extraction method by adopting aluminum sulfate as leaching agent | |
| CN102127641A (en) | Method for recovering scandium and titanium in titanium white wastewater | |
| CN102312098A (en) | Method for separation and purification of fluorescent grade yttrium oxide and europium oxide from waste phosphor powder | |
| CN1872377A (en) | Method for saponifying extraction agent | |
| CN102976525B (en) | Method for treating and recycling rare earth oxalate precipitation mother solution | |
| CN102965506B (en) | Method for removing aluminum from rare earth solution by benzoate precipitation method | |
| CN104928475A (en) | Recycling method of rare earth-containing aluminum silicon waste material | |
| CN104928504A (en) | Recycling method of rare earth in aluminum silicon waste | |
| CN102167467B (en) | Deep treatment technology of high-ammonia nitrogen rare earth wet process-smelted saponifying wastewater | |
| CN103755076B (en) | A kind of method of rare-earth industry waste water removing heavy metals | |
| CN111996396A (en) | Method for removing cerium and non-rare earth impurities from rare earth feed liquid | |
| CN106145443A (en) | A kind of processing method of Rare Earth Production waste water | |
| CN106336036A (en) | Method for recycling oxalic acid and hydrochloric acid in oxalic acid mother liquor | |
| US20230323509A1 (en) | Weak Acid Lixiviants for Recovery of Alkaline Earth Metals | |
| CN106244807B (en) | A method of the recovery purifying rare earth from ion adsorption type rare earth ore waste water | |
| CN108373249A (en) | A kind of high chlorine iron content waste sludge resource utilization method and its processing system | |
| CN107963648B (en) | Method for producing calcium carbonate from carbide slag by using phase transfer technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110824 Termination date: 20141105 |
|
| EXPY | Termination of patent right or utility model |