CN111115673A - Method for utilizing all components of caustic sludge - Google Patents
Method for utilizing all components of caustic sludge Download PDFInfo
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- CN111115673A CN111115673A CN201911426689.3A CN201911426689A CN111115673A CN 111115673 A CN111115673 A CN 111115673A CN 201911426689 A CN201911426689 A CN 201911426689A CN 111115673 A CN111115673 A CN 111115673A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/20—Halides
- C01F11/24—Chlorides
- C01F11/32—Purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
- C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
- C01B33/18—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
- C01F11/182—Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by an additive other than CaCO3-seeds
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/02—Magnesia
- C01F5/06—Magnesia by thermal decomposition of magnesium compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/10—Solid density
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Processing Of Solid Wastes (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention provides a method for utilizing all components of caustic sludge, belonging to the technical field of solid waste treatment. The method comprises the steps of finely dividing the components in the alkaline residue to prepare corresponding chemical products, mainly using the alkaline residue as a raw material, removing soluble salts through washing, converting carbonate and hydroxide phases into oxide phases through heat treatment, and respectively leaching through calcination and ammonium chloride solution and ammonium sulfate solution to better separate calcium and magnesium in the oxide phases; the obtained calcium chloride leaching liquor can be used for preparing high-purity calcium carbonate by a carbonization method, and the obtained magnesium sulfate leaching liquor can be used for preparing high-purity magnesium oxide by an ammonium carbonate precipitation method. Therefore, the method can realize the utilization of all components of the caustic sludge, can consume the caustic sludge on a large scale, realizes the cyclic utilization of the medium, reduces the cost, is energy-saving and environment-friendly, and is suitable for industrial production.
Description
Technical Field
The invention belongs to the technical field of solid waste treatment, and particularly relates to a method for utilizing all components of alkaline residue.
Background
The caustic sludge, also called white mud, is waste residue produced in the process of preparing soda ash by an ammonia-soda process, and about 300 kg of caustic sludge is produced for every 1 ton of soda ash produced. For the treatment of the caustic sludge, a stacking mode is usually adopted, the stacking and discharging of the caustic sludge cause serious resource waste and environmental pollution, and a large amount of caustic sludge forms a 'white sea' after being deposited, so that the pollution of surrounding soil and underground water is caused.
The main components and content of the caustic sludge depend on the components of the raw materials for producing the alkali. At present, the alkali-making process of each alkali factory is largely the same and slightly different, so the components of the alkali residue are basically similar, mainly comprising CaCO3、CaCl2、Mg(OH)2NaCl and the like, together with a small amount of SiO2、Al2O3And other salts, water insoluble, and the like.
With the enhancement of environmental protection consciousness of the whole society and the improvement of the attention degree on the development and utilization of secondary resources, the comprehensive utilization of the caustic sludge is paid extensive attention. At present, the main utilization methods of the caustic sludge comprise:
1) engineering building materials: alkali slag cement, alkali slag soil, alkali slag brick, building mortar modifier and the like;
2) in the chemical industry aspect: flue gas desulfurization, rubber packing and the like;
3) agriculture and fishery: soil conditioner or calcium-magnesium compound fertilizer, mariculture pond bottom or water quality conditioner, etc.;
4) and (3) environmental protection: treating red tide and water bloom, and preparing sterilizing health products and the like.
In the field of engineering building materials, the caustic sludge is difficult to be doped into building materials on a large scale due to high alkalinity and high chlorine content, so that the use amount of the caustic sludge is limited, and meanwhile, the durability and stability of the building materials are seriously influenced due to the fact that the caustic sludge contains a large amount of soluble salts and chloride ions; in other fields, the consumption of caustic sludge is greatly limited due to the limitation of the film regulation of the market.
Disclosure of Invention
The invention aims to provide a method for utilizing all components of alkaline residue, which can realize the utilization of all components of the alkaline residue and can absorb the alkaline residue on a large scale.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for utilizing all components of caustic sludge, which comprises the following steps:
mixing the alkaline residue with water, and sequentially and repeatedly washing and carrying out solid-liquid separation to obtain a liquid phase A and a solid phase B;
concentrating and crystallizing the liquid phase A to obtain sodium chloride and calcium chloride;
carrying out heat treatment on the solid phase B to obtain calcined powder;
mixing the calcined powder with an ammonium chloride solution, performing primary leaching, separating to obtain a solid precipitate C and a liquid phase D, adding a dispersing agent into the liquid phase D, introducing carbon dioxide gas, and carbonizing to obtain calcium carbonate;
mixing the solid precipitate C with an ammonium sulfate solution, heating to boil under stirring, performing secondary leaching, and performing solid-liquid separation after ammonia water is distilled to obtain a solid phase E and a liquid phase F; the solid phase E contains silicon dioxide;
and mixing the liquid phase F with an ammonium carbonate solution, precipitating to obtain magnesium carbonate, and calcining the magnesium carbonate to obtain magnesium oxide.
Preferably, in the water washing process, the solid-liquid ratio is 1: 2-5, the solid phase obtained by solid-liquid separation is repeatedly washed for 2-5 times, the filtrate obtained by washing each time is reused for 3-5 times until the solution density reaches more than 1.25g/mL, the reuse is stopped, and concentration and crystallization are carried out.
Preferably, the temperature of the heat treatment is 850 ℃ and the time is 1 h.
Preferably, the mass concentration of the ammonium chloride solution is 20%; the molar ratio of calcium oxide in the calcined powder to ammonium chloride in the ammonium chloride solution is 1: 2-3; the mass ratio of the calcined powder to water in the ammonium chloride solution is 1: 5-20.
Preferably, the time of the primary leaching is 5-20 min.
Preferably, the dispersing agent is sodium hexametaphosphate, and the using amount of the dispersing agent accounts for 0-3% of the mass of the liquid phase D.
Preferably, the mass ratio of the solid precipitate C to the ammonium sulfate solution is 1: 15-25, and the mass concentration of the ammonium sulfate solution is 10-20%.
Preferably, after the ammonia water is distilled, the volume of the obtained ammonia water is 20-80 mL.
Preferably, the mass concentration of the ammonium carbonate solution is 10%, and the temperature of the precipitation is 65 +/-3 ℃.
Preferably, the calcining temperature is 600-1500 ℃, and the calcining time is 2 h.
The invention provides a method for utilizing all components of caustic sludge, which comprises the following steps: the method comprises the following steps:
mixing the alkaline residue with water, and sequentially and repeatedly washing and carrying out solid-liquid separation to obtain a liquid phase A and a solid phase B; concentrating and crystallizing the liquid phase A to obtain sodium chloride and calcium chloride; carrying out heat treatment on the solid phase B to obtain calcined powder; mixing the calcined powder with an ammonium chloride solution, performing primary leaching, separating to obtain a solid precipitate C and a liquid phase D, adding a dispersing agent into the liquid phase D, introducing carbon dioxide gas, and carbonizing to obtain calcium carbonate; mixing the solid precipitate C with an ammonium sulfate solution, heating to boil under stirring, performing secondary leaching until ammonia water is distilled out, and performing solid-liquid separation to obtain a solid phase E and a liquid phase F; the solid phase E contains silicon dioxide; and mixing the liquid phase F with an ammonium carbonate solution, precipitating to obtain magnesium carbonate, and calcining the magnesium carbonate to obtain magnesium oxide. The method comprises the steps of finely dividing the components in the alkaline residue to prepare corresponding chemical products, mainly using the alkaline residue as a raw material, removing soluble salts through washing, converting carbonate and hydroxide phases into oxide phases through heat treatment, and respectively leaching through calcination and ammonium chloride solution and ammonium sulfate solution to better separate calcium and magnesium in the oxide phases; the obtained calcium chloride leaching liquor can be used for preparing high-purity calcium carbonate by a carbonization method, and the obtained magnesium sulfate leaching liquor can be used for preparing high-purity magnesium oxide by an ammonium carbonate precipitation method. Therefore, the method can realize the utilization of all components of the caustic sludge, can consume the caustic sludge on a large scale, realizes the cyclic utilization of the medium, reduces the cost, is energy-saving and environment-friendly, and is suitable for industrial production.
The ammonia gas generated in the process can be recovered through the ammonia absorber, and the ammonium salt can be recycled without polluting the environment.
Detailed Description
The invention provides a method for utilizing all components of caustic sludge, which comprises the following steps:
mixing the alkaline residue with water, and sequentially and repeatedly washing and carrying out solid-liquid separation to obtain a liquid phase A and a solid phase B;
concentrating and crystallizing the liquid phase A to obtain sodium chloride and calcium chloride;
carrying out heat treatment on the solid phase B to obtain calcined powder;
mixing the calcined powder with an ammonium chloride solution, performing primary leaching, separating to obtain a solid precipitate C and a liquid phase D, adding a dispersing agent into the liquid phase D, introducing carbon dioxide gas, and carbonizing to obtain calcium carbonate;
mixing the solid precipitate C with an ammonium sulfate solution, heating to boil under stirring, performing secondary leaching until ammonia water is distilled out, and performing solid-liquid separation to obtain a solid phase E and a liquid phase F; the solid phase E contains silicon dioxide;
and mixing the liquid phase F with an ammonium carbonate solution, precipitating to obtain magnesium carbonate, and calcining the magnesium carbonate to obtain magnesium oxide.
The invention mixes the caustic sludge with water, and sequentially and repeatedly carries out water washing and solid-liquid separation to obtain a liquid phase A and a solid phase B. In the invention, the alkaline residue is preferably waste residue generated in the process of preparing the soda ash by using an ammonia-soda process, and the alkaline residue used in the invention is sourced from a factory for producing the soda ash. In the embodiment of the present invention, the present invention preferably uses dry caustic sludge, that is, caustic sludge after drying, and the drying process is not particularly limited in the present invention. In the invention, the water washing is preferably carried out under stirring conditions, and the stirring time of each water washing is preferably 30 min; the rotation speed of the stirring is not particularly limited in the present invention, and a process well known in the art may be used. In the invention, in the water washing process, the solid-liquid ratio (namely the mass ratio of the alkaline residue to the water) is preferably 1: 2-5, more preferably 1: 3-4, the solid phase obtained by solid-liquid separation in each time is preferably repeatedly washed for 2-5 times (more preferably 3-4 times), the filtrate obtained by water washing in each time is preferably applied for 3-5 times until the solution density reaches more than 1.25g/mL, and the application is stopped, and subsequent concentration and crystallization are carried out. The solid-liquid separation method is not particularly limited in the present invention, and a solid-liquid separation method well known in the art may be selected, and for example, the solid-liquid separation method may specifically be filtration.
After a liquid phase A and a solid phase B are obtained, the liquid phase A is concentrated and crystallized to obtain sodium chloride and calcium chloride; and carrying out heat treatment on the solid phase B to obtain calcined powder. The process of the concentration and crystallization in the present invention is not particularly limited, and a process well known in the art may be selected. In the present invention, the temperature of the heat treatment is preferably 850 ℃ and the time is preferably 1 hour. The present invention converts carbonates and hydroxides in a solid phase into oxides by heat treatment, and the calcined powder mainly contains magnesium oxide and calcium oxide.
After calcined powder is obtained, the calcined powder is mixed with an ammonium chloride solution, primary leaching is carried out, a solid precipitate C and a liquid phase D are obtained after separation, a dispersing agent is added into the liquid phase D, carbon dioxide gas is introduced into the liquid phase D, and carbonization is carried out to obtain calcium carbonate. In the present invention, the mass concentration of the ammonium chloride solution is preferably 20%; the mol ratio of the calcium oxide in the calcined powder to the ammonium chloride in the ammonium chloride solution is preferably 1: 2-3, and more preferably 1: 2.5; the mass ratio of the calcined powder to water in the ammonium chloride solution is preferably 1: 5-20, and more preferably 1: 10-15. The mixing process is not particularly limited in the invention, and the raw materials can be uniformly mixed by selecting the process well known in the field. In the present invention, the primary leaching is preferably carried out under agitation conditions, and the rotation speed of the agitation is not particularly limited in the present invention, and the agitation speed well known in the art may be selected. In the invention, the time of primary leaching is preferably 5-20 min, more preferably 10-15 min, and the temperature of primary leaching is preferably 30-80 ℃, more preferably 50-60 ℃. The invention uses an ammonium chloride solution to leach calcium ions, the liquid phase D contains the calcium ions, and the solid precipitate C contains magnesium.
The separation process is not particularly limited in the present invention, and a process known in the art may be selected, and filtration is particularly preferable. In the invention, the dispersant is preferably sodium hexametaphosphate, and the dosage of the dispersant accounts for 0-3% by mass of the liquid phase D, and more preferably 1-2%. The invention utilizes the dispersant to promote the carbonization process of calcium ions. The flow rate of the carbon dioxide gas introduced in the present invention is not particularly limited, and may be any flow rate known in the art. In the present invention, the temperature of the carbonization is preferably 40 ℃ and the time is preferably 30 min.
After a solid precipitate C is obtained, mixing the solid precipitate C with an ammonium sulfate solution, heating to boil under the condition of stirring, performing secondary leaching until ammonia water is distilled out, and performing solid-liquid separation to obtain a solid phase E and a liquid phase F; the solid phase E contains silica. In the invention, the mass ratio of the solid precipitate C to the ammonium sulfate solution is preferably 1: 15-25, more preferably 1: 20, and the mass concentration of the ammonium sulfate solution is preferably 10-20%, more preferably 12-15%. The mixing process is not particularly limited in the invention, and the raw materials can be uniformly mixed by selecting the process well known in the field. The rotation speed of the stirring is not particularly limited in the present invention, and a process well known in the art may be selected. In the invention, after the ammonia water is distilled, the volume of the obtained ammonia water is preferably 20-80 mL, and more preferably 40-60 mL. The invention leaches and dissolves magnesium-containing substances in the solid precipitate C through ammonium sulfate solution. The solid-liquid separation method is not particularly limited in the present invention, and a solid-liquid separation method well known in the art may be selected, and for example, the solid-liquid separation method may specifically be filtration. In the present invention, the solid phase E contains silica, and the solid phase E may replace part of river sand.
After the liquid phase F is obtained, the liquid phase F is mixed with an ammonium carbonate solution for precipitation to obtain magnesium carbonate, and the magnesium carbonate is calcined to obtain magnesium oxide. In the present invention, the mass concentration of the ammonium carbonate solution is preferably 10%. The mixing process is not particularly limited in the invention, and the raw materials can be uniformly mixed by selecting the process well known in the field. In the invention, the liquid phase F contains magnesium ions, and the invention uses ammonium carbonate to precipitate the magnesium ions in the liquid phase F. In the invention, the temperature of the precipitation is preferably 65 +/-3 ℃, and the time is preferably 30-60 min.
Before the calcination, the magnesium carbonate is preferably filtered, washed, dried and crushed in sequence. The process of filtering, washing, drying and pulverizing is not particularly limited in the present invention, and a process well known in the art may be selected. In the invention, the calcination temperature is preferably 600-1500 ℃, more preferably 650-1000 ℃, and the calcination time is preferably 2 h. The present invention preferably performs the calcination in a high temperature box-type resistance furnace.
In the invention, ammonia gas generated in the whole process can be recovered through the ammonia absorber, and ammonium salt is recycled, so that the environmental pollution is avoided.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Adding 2000mL of tap water into 1000 g of dry caustic sludge, stirring for 30min, sequentially and repeatedly washing and filtering for 3 times, wherein the filtrate washed by water each time is used as a cleaning solvent for 3 times, the filtrate density reaches 1.28g/mL after 3 times of repeated washing to obtain a liquid phase A and a solid phase B, and concentrating and crystallizing the liquid phase A to obtain sodium chloride and calcium chloride, wherein 216g of sodium chloride and 197g of calcium chloride containing sodium chloride are obtained;
and (2) carrying out heat treatment on the solid phase B at 850 ℃ for 1h to obtain calcined powder, taking 100g of calcined powder, carrying out primary leaching for 20 minutes (50 ℃) by using an ammonium chloride solution with the mass concentration of 20% under the condition of stirring, wherein the mass of ammonium chloride in the ammonium chloride solution is 125g, (the molar ratio of calcium oxide in the calcined powder to ammonium chloride in the ammonium chloride solution is 1: 2.34), the mass ratio of the calcined powder to water in the ammonium chloride solution is 1: 5, filtering to obtain a solid precipitate C and a liquid phase D, introducing carbon dioxide gas into the liquid phase D, and carbonizing (40 ℃, 30min) to obtain calcium carbonate, wherein the leaching rate of calcium ions is 99.5%.
Mixing 25g of solid precipitate C with an ammonium sulfate solution (prepared from 500g of water and 84g of ammonium sulfate), heating to boil, performing secondary leaching until the volume of distilled ammonia water is 80mL, finishing the reaction, and filtering to obtain a solid phase E and a liquid phase F, wherein the leaching rate of magnesium ions in the liquid phase F reaches 99.0%; and mixing the liquid phase F with an ammonium carbonate solution with the mass fraction of 10%, precipitating for 45min at the temperature of (65 +/-3) DEG C to obtain magnesium carbonate, filtering, washing, drying and crushing the magnesium carbonate precipitate, and calcining for 2h at the temperature of 650 ℃ in a high-temperature box-type resistance furnace to obtain magnesium oxide.
The magnesium oxide product prepared in example 1 was subjected to content analysis according to a conventional method, and the results are shown in Table 1.
Table 1 analysis results of magnesium oxide sample prepared in example 1
As can be seen from Table 1, the magnesium oxide extracted from the caustic sludge by the method of the invention has high purity and less impurities, and can realize comprehensive utilization of all components of the caustic sludge.
According to the embodiment, the invention provides the method for utilizing the total components of the alkaline residue, which mainly utilizes the alkaline residue as the raw material, removes soluble salts through washing, converts carbonate and hydroxide phases into oxide phases through heat treatment, and better separates calcium and magnesium through calcination and leaching of ammonium chloride solution and ammonium sulfate solution respectively; the obtained calcium chloride leaching liquor can be used for preparing high-purity calcium carbonate by a carbonization method, and the obtained magnesium sulfate leaching liquor can be used for preparing high-purity magnesium oxide by an ammonium carbonate precipitation method. Therefore, the method can realize the utilization of all components of the caustic sludge, can consume the caustic sludge on a large scale, realizes the cyclic utilization of the medium, reduces the cost, is energy-saving and environment-friendly, and is suitable for industrial production.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. The method for utilizing all components of caustic sludge is characterized by comprising the following steps of:
mixing the alkaline residue with water, and sequentially and repeatedly washing and carrying out solid-liquid separation to obtain a liquid phase A and a solid phase B;
concentrating and crystallizing the liquid phase A to obtain sodium chloride and calcium chloride;
carrying out heat treatment on the solid phase B to obtain calcined powder;
mixing the calcined powder with an ammonium chloride solution, performing primary leaching, separating to obtain a solid precipitate C and a liquid phase D, adding a dispersing agent into the liquid phase D, introducing carbon dioxide gas, and carbonizing to obtain calcium carbonate;
mixing the solid precipitate C with an ammonium sulfate solution, heating to boil under stirring, performing secondary leaching, and performing solid-liquid separation after ammonia water is distilled to obtain a solid phase E and a liquid phase F; the solid phase E contains silicon dioxide;
and mixing the liquid phase F with an ammonium carbonate solution, precipitating to obtain magnesium carbonate, and calcining the magnesium carbonate to obtain magnesium oxide.
2. The method according to claim 1, wherein in the water washing process, the solid-liquid ratio is 1: 2-5, the solid phase obtained by solid-liquid separation is repeatedly washed with water for 2-5 times, the filtrate obtained by each water washing is reused for 3-5 times until the solution density reaches more than 1.25g/mL, and the reuse is stopped for concentration and crystallization.
3. The method according to claim 1, wherein the temperature of the heat treatment is 850 ℃ and the time is 1 h.
4. The method according to claim 1, wherein the mass concentration of the ammonium chloride solution is 20%; the molar ratio of calcium oxide in the calcined powder to ammonium chloride in the ammonium chloride solution is 1: 2-3; the mass ratio of the calcined powder to water in the ammonium chloride solution is 1: 5-20.
5. The method according to claim 1 or 4, wherein the primary leaching time is 5-20 min.
6. The method according to claim 1, wherein the dispersant is sodium hexametaphosphate, and the dispersant is used in an amount of 0 to 3% by mass based on the liquid phase D.
7. The method as claimed in claim 1, wherein the mass ratio of the solid precipitate C to the ammonium sulfate solution is 1: 15-25, and the mass concentration of the ammonium sulfate solution is 10-20%.
8. The method according to claim 1 or 7, wherein the volume of the obtained ammonia water is 20-80 mL after the ammonia water is distilled.
9. The method according to claim 1, wherein the mass concentration of the ammonium carbonate solution is 10% and the temperature of the precipitation is 65 ± 3 ℃.
10. The method according to claim 1, wherein the calcining temperature is 600-1500 ℃, and the calcining time is 2 h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911426689.3A CN111115673A (en) | 2019-12-31 | 2019-12-31 | Method for utilizing all components of caustic sludge |
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| CN201911426689.3A CN111115673A (en) | 2019-12-31 | 2019-12-31 | Method for utilizing all components of caustic sludge |
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| CN111115673A true CN111115673A (en) | 2020-05-08 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111394581A (en) * | 2020-04-30 | 2020-07-10 | 舒新前 | Method for removing harmful components in iron-containing solid waste |
| CN114702051A (en) * | 2022-06-06 | 2022-07-05 | 潍坊泽隆新材料有限公司 | Method for producing superfine high-activity magnesium oxide by using by-product magnesium carbonate filter cake |
| CN115594528A (en) * | 2022-08-26 | 2023-01-13 | 关祥瑞（Cn） | Method and equipment for preparing composite amino acid calcium magnesium chelating solution by using ammonia-soda alkaline residue |
-
2019
- 2019-12-31 CN CN201911426689.3A patent/CN111115673A/en not_active Withdrawn
Non-Patent Citations (3)
| Title |
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| 孙歌东等: "蒸氨废液废渣治理综合利用", 《河南化工》 * |
| 张倍维等: "碱厂白泥生产沉淀碳酸钙的研究进展", 《广西轻工业》 * |
| 白云山等: "铵浸法由白云石制备高纯度碳酸钙和氧化镁", 《无机盐工业》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111394581A (en) * | 2020-04-30 | 2020-07-10 | 舒新前 | Method for removing harmful components in iron-containing solid waste |
| CN114702051A (en) * | 2022-06-06 | 2022-07-05 | 潍坊泽隆新材料有限公司 | Method for producing superfine high-activity magnesium oxide by using by-product magnesium carbonate filter cake |
| CN115594528A (en) * | 2022-08-26 | 2023-01-13 | 关祥瑞（Cn） | Method and equipment for preparing composite amino acid calcium magnesium chelating solution by using ammonia-soda alkaline residue |
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