CN101760646A - Leaching method of magnesium-containing ore - Google Patents
Leaching method of magnesium-containing ore Download PDFInfo
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- CN101760646A CN101760646A CN200810240925A CN200810240925A CN101760646A CN 101760646 A CN101760646 A CN 101760646A CN 200810240925 A CN200810240925 A CN 200810240925A CN 200810240925 A CN200810240925 A CN 200810240925A CN 101760646 A CN101760646 A CN 101760646A
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Abstract
The invention provides a leaching method of a magnesium-containing ore. The method comprises the following steps: mixing the magnesium-containing ore with sulfuric acid solution and performing acid leaching to obtain leaching solution containing magnesium sulfate; purifying the leaching solution to obtain magnesium sulfate solution; mixing the magnesium sulfate solution with ammonium bicarbonate to obtain solution which contains magnesium hydrogen carbonate and residual magnesium sulfate; heating the solution and disintegrating the magnesium hydrogen carbonate to produce basic magnesium carbonate precipitation and carbon dioxide; and heating serous fluid which contains the basic magnesium carbonate precipitation and then performing filtering separation on the serous fluid to obtain the basic magnesium carbonate precipitation and filter liquor. By utilizing the leaching method of the magnesium-containing ore of the invention, not only the metal in the ore can be recovered, but also the magnesium in the ore can be efficiently recovered and the pollution is reduced.
Description
Technical field
The present invention relates to wet method smelting process, especially relate to a kind of leaching method of magnesium-containing ore.
Background technology
Ore smelting is traditionally undertaken by pyrometallurgical smelting process.Developed wet process smelting technique in recent years.Because hydrometallurgy can reduce the pollution to environment effectively, and can be suitable for multiple different ore deposit, therefore replace pyrometallurgical smelting just gradually.
Present wet method smelting process adopts sulphuric acid solvent extraction method more, the multiple metallic element that can leach in the ore to be contained.If can not reclaim, will be great waste, and some composition in the leach liquor also may damage to human body to these metallic elements.When for example magnesium-containing ore being leached, can produce the solution that contains sal epsom in a large number, because sal epsom is known as " misery " again, be the toxic substance that can cause that the people suffers from diarrhoea, and therefore country forbids containing the direct discharging of waste water of sal epsom.Traditional treatment process is that the solution that will contain sal epsom carries out heating evaporation, obtains magnesium sulfate crystals.But the shortcoming of this treatment process is the cost height, and efficient is low, need to consume a large amount of energy, and the purity of resulting magnesium sulfate crystals is low.
For example, Chinese patent CN101104521 discloses a kind of treatment process of sal epsom waste liquid, and it comprises: measure a certain amount of sal epsom waste liquid, under the mechanical stirring condition, heat condensing crystal, crystallization after drying, calcining, the primary oxidation magnesium that obtains, the flue gas of generation reclaims, and uses as system sulfuric acid; The primary oxidation magnesium that obtains is added water digestion, filtering and impurity removing, obtain magnesium hydroxide emulsion, move into emulsion in the reactor and control pressure, logical carbonic acid gas carbonization under agitation condition, after filtration, obtain magnesium bicarbonate solution, under heating and agitation condition, carry out the magnesium bicarbonate solution pyrolysis and just obtain the basic carbonate magnesium precipitate, filter at last, wash, dry and calcine, obtain activated magnesia.
Because this technology adopts evaporation-incinerating operational path, therefore, mass consumption the energy, environment caused once more polluted, and because methods such as this process using calcinings, so to the requirement height of equipment, and then the production cost height.
Summary of the invention
Purpose of the present invention is intended to one of solve the aforementioned problems in the prior at least.
One object of the present invention is to propose a kind of method for leaching magnesium-containing ore that can high efficiente callback magnesium.Leaching method according to the magnesium-containing ore of the embodiment of the invention may further comprise the steps:
A) magnesium-containing ore is mixed with sulphuric acid soln carry out acidleach to obtain leaching solution containing magnesium sulfate;
B) described leach liquor is purified obtain Adlerika;
C) Adlerika is mixed with bicarbonate of ammonia, obtain containing the solution of Magnesium hydrogen carbonate and residual magnesium sulfate;
D) described solution is heated, Magnesium hydrogen carbonate is decomposed, generate basic carbonate magnesium precipitate and carbonic acid gas;
E) the sedimentary slurries of magnesium basic carbonate that contain after the heating are carried out filtering separation, obtain basic carbonate magnesium precipitate and filtrate.
Method for leaching magnesium-containing ore according to an embodiment of the invention, metallic element in the magnesium-containing ore can be reclaimed, in addition, magnesium basic carbonate is a kind of important chemical product, and it can be used for the rubber item weighting agent, makes other magnesium salts, as the stopping composition of multiple light industrial goods, also be used to make high-efficiency insulated, refractory materials.By the magnesium oxide of magnesium basic carbonate through the calcining output, can also conduct inhibitor, the catalyzer in the chemical industry and pottery, enamel pharmaceutically except that possessing such use, the raw material of glass, in hydrometallurgy, can be used as the neutralization precipitation agent.Therefore, utilize the method for leaching magnesium-containing ore of this embodiment, can reduce the processing cost of wastewater treatment, and bring certain economic benefits, provide a kind of new technology for the protection environment with developing a circular economy simultaneously.
According to embodiments of the invention, method for leaching magnesium-containing ore of the present invention also has following additional technical feature:
In one embodiment of the invention, also comprise to separate the magnesium basic carbonate that obtains be deposited in to calcine under 900 ℃ and obtain magnesium oxide.Like this, can obtain magnesium oxide by under 900 ℃, magnesium basic carbonate effectively being calcined.In further embodiment of the present invention, before the basic carbonate magnesium precipitate is calcined, it is washed, and washings is mixed with described filtrate.Like this, can improve the basic carbonate magnesium precipitate is calcined the magnesian purity of acquisition, can will reclaim simultaneously, improve the rate of recovery of magnesium attached to the sal epsom on the basic carbonate magnesium precipitate.
In one embodiment of the invention, use calcium hydroxide and/or calcium oxide that described filtrate is carried out causticization, obtain containing the slurries of magnesium hydrate precipitate and calcium sulfate, and generate receipts ammonia.According to the method for this embodiment, can the magnesium in the filtrate be reclaimed, further improved the organic efficiency of magnesium.In the further embodiment of the present invention, carbonic acid gas and water reaction generation bicarbonate of ammonia that the ammonia that generated and Magnesium hydrogen carbonate are decomposed.Like this, can reclaim ammonia, carbonic acid gas, and the bicarbonate of ammonia of having regenerated, reduced cost, alleviated the pressure of ammonia to environment.In another further embodiment of the present invention, also comprise: in the described slurries that contain magnesium hydroxide and calcium sulfate, feed carbonic acid gas, obtain containing the slurries of Magnesium hydrogen carbonate and calcium sulfate; The separating calcium sulphate precipitation heats the magnesium bicarbonate solution of isolating calcium sulfate precipitation, makes Magnesium hydrogen carbonate decompose, and generates magnesium basic carbonate and carbonic acid gas; And described magnesium basic carbonate carried out calcining under 900 ℃ obtain magnesium oxide.Can further improve organic efficiency like this, and obtain magnesium oxide magnesium in the Adlerika.In another further embodiment of the present invention, also comprise: the described slurries that contain magnesium hydroxide and calcium sulfate are carried out pickling obtain calcium sulfate precipitation and Adlerika; The separating calcium sulphate precipitation; And the Adlerika crystallization that will isolate calcium sulfate precipitation obtains the magnesium sulfate heptahydrate crystal.Can further improve organic efficiency like this, and obtain the magnesium sulfate heptahydrate crystal magnesium in the Adlerika.
In one embodiment of the invention, the Adlerika that contains Magnesium hydrogen carbonate being carried out add the magnesium basic carbonate crystal seed in the heat-processed, can change the size of crystallization crystal grain like this, to satisfy the requirement of different size magnesium products.
In one embodiment of the invention, the Adlerika that contains Magnesium hydrogen carbonate is being carried out adding ammoniacal liquor in the heat-processed.Can further improve the productive rate of magnesium basic carbonate like this.
In one embodiment of the invention, described purification comprises at least a in iron, aluminium, cobalt, nickel and the manganese of removing in the leach liquor.Thus, not only can reclaim valuable metal compositions such as iron, aluminium, cobalt, nickel and manganese, and reclaim the magnesium in the ore, both reduce pollution, again recycle resource.
Additional aspect of the present invention and advantage part in the following description provide, and part will become obviously from the following description, or recognize by practice of the present invention.
Description of drawings
Fig. 1 is the schema of leaching method of the magnesium-containing ore of first embodiment of the invention;
Fig. 2 is the schema of leaching method of the magnesium-containing ore of second embodiment of the invention;
Fig. 3 is the schema of leaching method of the magnesium-containing ore of third embodiment of the invention;
Fig. 4 is the schema of leaching method of the magnesium-containing ore of fourth embodiment of the invention;
Fig. 5 is the schema of leaching method of the magnesium-containing ore of fifth embodiment of the invention;
Fig. 6 is the schema of leaching method of the magnesium-containing ore of sixth embodiment of the invention.
Embodiment
Describe embodiments of the invention below in detail, the example of described embodiment is shown in the drawings, is exemplary below by the embodiment that is described with reference to the drawings, and only is used to explain the present invention, and can not be interpreted as limitation of the present invention.
Need to prove that the term that is adopted " calcium hydroxide and/or calcium oxide " is meant and can uses calcium oxide (unslaked lime is called slaked lime and uses after the digestion) in the present invention, also can use calcium hydroxide (white lime), also can use the mixture of the two.In actually operating, can water assimilation of quicklime using (CaO), thus obtaining milk of lime utilization, principal reaction is CaO+H
2O=Ca (OH)
2
Fig. 1 shows the schema of the leaching method of magnesium-containing ore according to an embodiment of the invention.The leaching method of magnesium-containing ore comprises following step according to an embodiment of the invention:
At first magnesium-containing ore is mixed with sulphuric acid soln and carry out acidleach to obtain leaching solution containing magnesium sulfate, the reaction of generation is as follows:
MgO+H
2SO
4＝MgSO
4+H
2O；
Then, described leach liquor is purified obtain Adlerika.
The sulfuric acid extract technology that is adopted among the present invention is not subjected to any restriction.For example, leaching can be leached or the leaching of oxygen enrichment high pressure for the oxygen enrichment normal pressure.Leaching process comprises magniferous nickel sulfide ore of fine grinding or nickel-containing eluvial ore (for example high magnesium nickel ore concentrate); Carry out pulp with the high magnesium nickel ore concentrate of sulphuric acid soln after to fine grinding; Concentrate after the pulp joined leach in the container, wherein leaching temperature in the container, to be controlled to be 90 ℃-100 ℃, pressure be normal pressure, and aerating oxygen leaches so that carry out the oxygen enrichment normal pressure in leaching container simultaneously.Before the leach liquor that contains sal epsom is reclaimed magnesium, leach liquor is purified.
Employed in the present invention term " purification " can be at least a in iron, aluminium, cobalt, nickel and the manganese of removing in (or reclaim) sulphuric leachate, but the present invention is not limited to remove mentioned component.For example, with reference to figure 6, in one embodiment of the invention, the leach liquor that the oxygen enrichment normal pressure is directly leached generation is discharged in leaching container the heavy iron container, with the temperature regulation to 75 of leach liquor ℃～80 ℃, and for example 78 ℃, and the pH value of leach liquor is adjusted to 3～4, thereby precipitation is tapped a blast furnace.Because the purification in the sulfuric acid extract technology is that those of ordinary skills are known, gives unnecessary details no longer in detail here.
Next, Adlerika is mixed with ammonium bicarbonate soln, makes sal epsom and bicarbonate of ammonia that following reaction take place:
MgSO
4+2NH
4HCO
3＝Mg(HCO
3)
2+(NH
4)
2SO
4
Generated Magnesium hydrogen carbonate like this.Generally, bicarbonate of ammonia does not consume the whole sal epsom in the Adlerika, has therefore obtained to contain the solution of Magnesium hydrogen carbonate and remaining unreacted sal epsom.
Then, the described solution that contains Magnesium hydrogen carbonate and sal epsom is heated, makes Magnesium hydrogen carbonate generation pyrolysis to generate the basic carbonate magnesium precipitate, react as follows:
5Mg(HCO
3)
2＝4MgCO
3·Mg(OH)
2↓+6CO
2↑
At last, by carrying out filtering separation, obtain basic carbonate magnesium precipitate and the filtrate of containing remaining unreacted sal epsom to containing the sedimentary slurries of magnesium basic carbonate.
By aforesaid method, can reach the magnesium in the magnesium-containing ore is effectively reclaimed.Described magniferous ore for example is magniferous nickel sulfide ore or nickel-containing eluvial ore.
In one embodiment of the invention, in Magnesium hydrogen carbonate generation pyrolytic reaction process, can in its reaction system, add the magnesium basic carbonate crystal seed, can change the magnesium basic carbonate crystalline grain-size that generates like this, to satisfy the demand of different size magnesium products.In another embodiment, ammoniacal liquor can also be in reaction system, added, the productive rate of magnesium basic carbonate can be improved like this.The magnesium basic carbonate that is obtained can directly be used as commodity selling, obtains bigger economic benefit.
In addition, also can carry out deep processing to magnesium basic carbonate, according to shown in Figure 2, to separate the basic carbonate magnesium precipitate that obtains calcine and obtain magnesium oxide.The reaction that is taken place is as follows:
4MgCO
3·Mg(OH)
2·4H
2O＝5MgO+4CO
2↑+5H
2O
In one embodiment of the invention, can be under 900 ℃ the basic carbonate magnesium precipitate be calcined and obtain magnesium oxide, resulting like this magnesium oxide purity is high to be fit to commercially, has obtained bigger economic benefit.In another one embodiment of the present invention, before the basic carbonate magnesium precipitate is calcined, at first it is washed, like this, can improve the basic carbonate magnesium precipitate is calcined the magnesian purity of acquisition, simultaneously washings be mixed with aforesaid filtrate, will reclaim attached to the sal epsom on the basic carbonate magnesium precipitate, by subsequent disposal, improve the rate of recovery of magnesium.
Because the ammonium sulfate that in aforesaid filtrate, contains remaining unreacted sal epsom and generated, for magnesium and ammonium salt that it contained are reclaimed, with reference to figure 3, in one embodiment of the invention, with filtrate and calcium hydroxide and/or calcium oxide generation causticizing reaction, react as follows:
(NH
4)
2SO
4+MgSO
4+2Ca(OH)
2＝2CaSO
4↓+Mg(OH)
2↓+2NH
3↑+2H
2O
Like this, generated the slurries that contain magnesium hydroxide and calcium sulfate, and ammonium salt has been converted into ammonia (NH
3).In one embodiment, with the ammonia (NH that is generated in the causticizing reaction
3) with other steps (as step B) and/or magnesium basic carbonate calcination process in) carbonic acid gas and the water reaction generation bicarbonate of ammonia that are generated.React as follows:
CO
2+NH
3+H
2O＝NH
4HCO
3
Like this, can reclaim ammonia, carbonic acid gas, and the bicarbonate of ammonia of having regenerated, reduced cost, alleviated the pressure of ammonia to environment.
In addition, in causticizing reaction, generated calcium sulfate precipitation and magnesium hydrate precipitate, can obtain gypsum (calcium sulfate) and magnesium hydroxide by calcium sulfate precipitation is separated.The method of separating calcium sulphate and magnesium hydroxide can be known any method in the prior art, for example, can adopt in one embodiment of the invention and in the causticizing reaction system, add the calcium sulfate crystal seed, therefore, when sal epsom and calcium hydroxide reacted, formed calcium sulfate precipitation can be formed on the crystal seed, thereby the granularity of calcium sulfate precipitation can further increase, promptly form the calcium sulfate precipitation of volume particle size, be convenient to separating between follow-up calcium sulfate and the magnesium hydrate precipitate thus.In another embodiment of the present invention, as shown in Figure 4,, magnesium hydrate precipitate can be converted into the relatively large Magnesium hydrogen carbonate of solubleness, react as follows by feeding carbonic acid gas to the slurries that contain magnesium hydroxide and calcium sulfate:
Mg(OH)
2+CaSO
4+CO
2＝MgHCO
3+CaSO
4↓+H
2O
Further, the separating calcium sulphate precipitation heats the magnesium bicarbonate solution of isolating calcium sulfate precipitation, makes Magnesium hydrogen carbonate decompose, and it is as follows to generate magnesium basic carbonate and carbon dioxide reaction:
5Mg(HCO
3)
2＝4MgCO
3·Mg(OH)
2↓+6CO
2↑
Then, carry out under 900 ℃, calcining and to the magnesium basic carbonate that is generated and obtain magnesium oxide.Like this, can improve the efficient that magnesium is reclaimed, and obtain the magnesium oxide product of better economic benefit.
In addition, in another embodiment of the present invention, as shown in Figure 5, can carry out pickling, react as follows the slurries that contain magnesium hydroxide and calcium sulfate:
CaSO
4+Mg(OH)
2+H
2SO
4＝CaSO
4↓+MgSO
4+2H
2O
Can reach separating like this to sal epsom and calcium sulfate, after the separating calcium sulphate precipitation, obtained the higher Adlerika of purity, by Adlerika is carried out crystallization, for example can obtain the crystal of magnesium sulfate heptahydrate, further improve the organic efficiency of magnesium by reduction vaporization, cooling crystallization method.
Concrete example according to the embodiment of the invention is described below.
Example 1
Table 1 contains the leach liquor component list (g/L) of sal epsom, and wherein Adlerika is that the sulphuric leachate of magnesium-containing ore obtains through after purifying.
| Mg | SO 4 2- | Al | Ni | Co | Mn | Fe |
| 26-40 | 103～158 | 0.023 | 0.004 | 0.0016 | 0.0024 | 0.002 |
Ammoniacal liquor: 10～25% concentration ammoniacal liquor
Get the leach liquor 500mL that contains sal epsom of table 1
NH
4HCO
31.0～1.2 times of theoretical amount
Adding mode: NH
4HCO
3The aqueous solution adds and contains in the leach liquor of sal epsom
Temperature of reaction: 50～40 ℃
Reaction times: 0.5 hour
Pyrolysis temperature: 60 ℃～95 ℃
Pyrolysis time: 0.5 hour
In the Mg productive rate: 70～75%
Product purity: 〉=98%
Example 2.
Get the leach liquor 500mL that contains sal epsom of table 1
Solid NH
4HCO
31.0～1.2 times of theoretical amount
Adding mode: solid NH
4HCO
3The aqueous solution joins in the leach liquor that contains sal epsom
Temperature of reaction: normal temperature
Reaction times: 0.5 hour
Pyrolysis temperature: 60 ℃～95 ℃
Pyrolysis time: 0.5 hour
Filtration time: 0.5 minute～5 minutes
In the Mg productive rate: 70～75%
Product purity: 〉=98%
Example 3
Get the leach liquor 500mL that contains sal epsom of table 1
NH
4HCO
31.1 times of theoretical amount
Ammoniacal liquor: 25% concentration ammoniacal liquor 5mL
Adding mode: NH
4HCO
3And ammoniacal liquor joins in the leach liquor that contains sal epsom
Reaction times: 0.5 hour
Pyrolysis temperature: 60 ℃～95 ℃
Pyrolysis time: 0.5 hour
In the Mg productive rate: 80～85%
Product purity: 〉=98%
Example 4
Get the filtered liquid and the about 500mL of washings of example 1
Add previously prepared gypsum (calcium sulfate) crystal seed
The lime milk excessive 1.05 of working concentration 5～20 weight %.
The causticization time: 1～2 hour
Causticization temperature: normal temperature～40 ℃
Separate gypsum (calcium sulfate) and magnesium hydroxide, filtrate ammonia still process:
Temperature: 80～100 ℃
Time: 1～2h
Ammonia recovery: 98%
Gypsum pickling: pH2～2.5
Output gypsum purity: 〉=95%
Mg：≤0.5-1％
Example 5
Mg (OH) with example 4 outputs
2Flocculate into 30% ore pulp.
Feed CO
20～0.4Mpa keep-ups pressure
The calcification time: about 1 hour
Filter output MgHCO
3Solution.
Example 6.
MgHCO with example 5
3The solution decompression pyrolysis
Temperature: 60 ℃～102 ℃
Time: 1～2 hour
Filter and generate 4MgCO
3Mg (OH)
24H
2The O precipitation.
Example 7
4MgCO with example 6 outputs
3Mg (OH)
24H
2O precipitation, oven dry, calcining output MgO.
MgO content: 〉=95%
CaO content :≤0.5%
Example 8
The NH that contains with example 4 outputs
3, CO
2Steam H
2O absorbs to generate and contains NH
4HCO
3The aqueous solution returns usefulness.
Example 9.
The magnesium basic carbonate of example 1 or example 2 was dewatered 1～2 hour for 80～100 ℃, generate anhydrous magnesium basic carbonate and be MgO through calcining
Calcination time: 1～3 hour
Calcining temperature: 900～950 ℃
Output MgO purity: 〉=95%
CaO content :≤0.5%
Meet lightweight MgO and active MgO specification of quality.
Although illustrated and described embodiments of the invention, for the ordinary skill in the art, be appreciated that without departing from the principles and spirit of the present invention and can carry out multiple variation, modification, replacement and modification that scope of the present invention is by claims and be equal to and limit to these embodiment.
Claims (10)
1. the leaching method of a magnesium-containing ore may further comprise the steps:
A) magnesium-containing ore is mixed with sulphuric acid soln carry out acidleach to obtain leaching solution containing magnesium sulfate;
B) described leach liquor is purified obtain Adlerika;
C) Adlerika is mixed with bicarbonate of ammonia, obtain containing the solution of Magnesium hydrogen carbonate and residual magnesium sulfate;
D) described solution is heated, Magnesium hydrogen carbonate is decomposed, generate basic carbonate magnesium precipitate and carbonic acid gas;
E) the sedimentary slurries of magnesium basic carbonate that contain after the heating are carried out filtering separation, obtain basic carbonate magnesium precipitate and filtrate.
2. the method that reclaims magnesium from Adlerika according to claim 1 is characterized in that, further comprises: the isolating magnesium basic carbonate that obtains of institute is deposited in to calcine under 900 ℃ and obtains magnesium oxide.
3. the method that reclaims magnesium from Adlerika according to claim 2 is characterized in that, before the basic carbonate magnesium precipitate is calcined it is washed, and washings is mixed with described filtrate.
4. the method that reclaims magnesium from Adlerika according to claim 1 is characterized in that, further comprises: with calcium hydroxide and/or calcium oxide described filtrate is carried out causticization, obtain containing the slurries of magnesium hydrate precipitate and calcium sulfate, and generate ammonia.
5. the method that reclaims magnesium from Adlerika according to claim 4 is characterized in that, with described ammonia and step D) middle carbonic acid gas that generates and water reaction generation bicarbonate of ammonia.
6. the method that reclaims magnesium from Adlerika according to claim 4 is characterized in that, further comprises:
In the described slurries that contain magnesium hydroxide and calcium sulfate, feed carbonic acid gas, obtain containing the slurries of Magnesium hydrogen carbonate and calcium sulfate;
The separating calcium sulphate precipitation;
The solution of isolating calcium sulfate is heated, make Magnesium hydrogen carbonate decompose, generate magnesium basic carbonate and carbonic acid gas; And
Described magnesium basic carbonate carried out calcining under 900 ℃ obtain magnesium oxide.
7. the method that reclaims magnesium from Adlerika according to claim 4 is characterized in that, further comprises:
The described slurries that contain magnesium hydroxide and calcium sulfate are carried out pickling obtain calcium sulfate precipitation and Adlerika;
The separating calcium sulphate precipitation; And
Make the Adlerika crystallization of isolating calcium sulfate precipitation prepare the magnesium sulfate heptahydrate crystal.
8. the method that reclaims magnesium from Adlerika according to claim 1 is characterized in that, at step D) in adding magnesium basic carbonate crystal seed.
9. the method that reclaims magnesium from Adlerika according to claim 1 is characterized in that, at step D) in adding ammoniacal liquor.
10. the leaching method of magnesium-containing ore according to claim 1 is characterized in that, described purification comprises at least a in iron, aluminium, cobalt, nickel and the manganese of removing in the leach liquor.
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|---|---|---|---|
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|---|---|---|---|
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102392143A (en) * | 2011-10-28 | 2012-03-28 | 东北大学 | Recycling method of magnesium in silicate nickel oxide ore |
| CN102634680A (en) * | 2012-05-03 | 2012-08-15 | 长春黄金研究院 | Method for comprehensively recovering magnesium during process of extracting gold from magnesium-containing gold ore pile |
| CN106219580A (en) * | 2016-07-25 | 2016-12-14 | 成都市新都化工股份有限公司 | A kind of method preparing basic magnesium carbonate |
| CN111394598A (en) * | 2020-03-30 | 2020-07-10 | 龙岩紫云化学科技有限公司 | Method for extracting magnesium and co-producing calcium sulfate from magnesium-containing carbonate ore |
| CN111549239A (en) * | 2019-02-08 | 2020-08-18 | 北京中金瑞丰环保科技有限公司 | Resourceful treatment method of magnesium-containing raw material |
| CN115108570A (en) * | 2022-06-17 | 2022-09-27 | 中南大学 | Process for preparing basic magnesium carbonate and ammonium sulfate by innocent treatment in manganese-containing wastewater |
| CN115385366A (en) * | 2022-09-01 | 2022-11-25 | 广东邦普循环科技有限公司 | Treatment method of magnesium-containing waste liquid |
| CN115432724A (en) * | 2022-10-27 | 2022-12-06 | 绵阳师范学院 | Resourceful treatment method of waste ammonium magnesium salt |
-
2008
- 2008-12-24 CN CN200810240925A patent/CN101760646A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102392143A (en) * | 2011-10-28 | 2012-03-28 | 东北大学 | Recycling method of magnesium in silicate nickel oxide ore |
| CN102392143B (en) * | 2011-10-28 | 2013-08-21 | 东北大学 | Recycling method of magnesium in silicate nickel oxide ore |
| CN102634680A (en) * | 2012-05-03 | 2012-08-15 | 长春黄金研究院 | Method for comprehensively recovering magnesium during process of extracting gold from magnesium-containing gold ore pile |
| CN106219580A (en) * | 2016-07-25 | 2016-12-14 | 成都市新都化工股份有限公司 | A kind of method preparing basic magnesium carbonate |
| CN111549239A (en) * | 2019-02-08 | 2020-08-18 | 北京中金瑞丰环保科技有限公司 | Resourceful treatment method of magnesium-containing raw material |
| CN111549239B (en) * | 2019-02-08 | 2022-04-22 | 北京中金瑞丰环保科技有限公司 | Resourceful treatment method of magnesium-containing raw material |
| CN111394598A (en) * | 2020-03-30 | 2020-07-10 | 龙岩紫云化学科技有限公司 | Method for extracting magnesium and co-producing calcium sulfate from magnesium-containing carbonate ore |
| CN115108570A (en) * | 2022-06-17 | 2022-09-27 | 中南大学 | Process for preparing basic magnesium carbonate and ammonium sulfate by innocent treatment in manganese-containing wastewater |
| CN115385366A (en) * | 2022-09-01 | 2022-11-25 | 广东邦普循环科技有限公司 | Treatment method of magnesium-containing waste liquid |
| CN115385366B (en) * | 2022-09-01 | 2024-05-10 | 广东邦普循环科技有限公司 | Treatment method of magnesium-containing waste liquid |
| CN115432724A (en) * | 2022-10-27 | 2022-12-06 | 绵阳师范学院 | Resourceful treatment method of waste ammonium magnesium salt |
| CN115432724B (en) * | 2022-10-27 | 2023-11-21 | 绵阳师范学院 | Recycling treatment method of magnesium ammonium waste salt |
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Application publication date: 20100630 |