CN102627305A - Method using alkaline process to extract alumina in coal ash - Google Patents
Method using alkaline process to extract alumina in coal ash Download PDFInfo
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- CN102627305A CN102627305A CN2012100849156A CN201210084915A CN102627305A CN 102627305 A CN102627305 A CN 102627305A CN 2012100849156 A CN2012100849156 A CN 2012100849156A CN 201210084915 A CN201210084915 A CN 201210084915A CN 102627305 A CN102627305 A CN 102627305A
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- Prior art keywords
- alumina
- flyash
- liquid
- alkaline process
- process according
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Links
- 238000000034 method Methods 0.000 title claims abstract description 100
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 239000010883 coal ash Substances 0.000 title abstract description 6
- 238000002386 leaching Methods 0.000 claims abstract description 61
- 239000007790 solid phase Substances 0.000 claims abstract description 49
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 239000007787 solid Substances 0.000 claims abstract description 33
- 239000003513 alkali Substances 0.000 claims abstract description 30
- 239000002994 raw material Substances 0.000 claims abstract description 25
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 22
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 22
- 239000004571 lime Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000002002 slurry Substances 0.000 claims abstract description 13
- 235000019738 Limestone Nutrition 0.000 claims abstract description 12
- 239000006028 limestone Substances 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 238000010304 firing Methods 0.000 claims abstract description 5
- 239000010881 fly ash Substances 0.000 claims description 56
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 41
- 239000000284 extract Substances 0.000 claims description 37
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Substances [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 23
- 238000001704 evaporation Methods 0.000 claims description 20
- 230000008020 evaporation Effects 0.000 claims description 20
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 20
- 235000017550 sodium carbonate Nutrition 0.000 claims description 20
- 238000000354 decomposition reaction Methods 0.000 claims description 19
- 239000000843 powder Substances 0.000 claims description 19
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 18
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 18
- 238000002360 preparation method Methods 0.000 claims description 12
- 239000004568 cement Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 8
- 238000010276 construction Methods 0.000 claims description 7
- 238000000605 extraction Methods 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 4
- 239000006210 lotion Substances 0.000 claims description 3
- 239000012452 mother liquor Substances 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 abstract 2
- 229910021502 aluminium hydroxide Inorganic materials 0.000 abstract 2
- 239000011734 sodium Substances 0.000 description 29
- 229910052708 sodium Inorganic materials 0.000 description 14
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 11
- 239000000203 mixture Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 7
- 239000003518 caustics Substances 0.000 description 7
- 239000002893 slag Substances 0.000 description 7
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 7
- 229910001948 sodium oxide Inorganic materials 0.000 description 7
- 239000002253 acid Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 229910052782 aluminium Inorganic materials 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 230000035800 maturation Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 159000000013 aluminium salts Chemical class 0.000 description 1
- 229910000329 aluminium sulfate Inorganic materials 0.000 description 1
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 239000001506 calcium phosphate Substances 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 229910052863 mullite Inorganic materials 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000012254 powdered material Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 1
- 229940078499 tricalcium phosphate Drugs 0.000 description 1
- 229910000391 tricalcium phosphate Inorganic materials 0.000 description 1
- 235000019731 tricalcium phosphate Nutrition 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/0693—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process from waste-like raw materials, e.g. fly ash or Bayer calcination dust
-
- 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
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/0613—Pretreatment of the minerals, e.g. grinding
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B18/00—Use of agglomerated or waste materials or refuse as fillers for mortars, concrete or artificial stone; Treatment of agglomerated or waste materials or refuse, specially adapted to enhance their filling properties in mortars, concrete or artificial stone
- C04B18/04—Waste materials; Refuse
- C04B18/06—Combustion residues, e.g. purification products of smoke, fumes or exhaust gases
- C04B18/08—Flue dust, i.e. fly ash
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B28/00—Compositions of mortars, concrete or artificial stone, containing inorganic binders or the reaction product of an inorganic and an organic binder, e.g. polycarboxylate cements
- C04B28/02—Compositions of mortars, concrete or artificial stone, containing inorganic binders or the reaction product of an inorganic and an organic binder, e.g. polycarboxylate cements containing hydraulic cements other than calcium sulfates
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/04—Working-up slag
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/91—Use of waste materials as fillers for mortars or concrete
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Ceramic Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Materials Engineering (AREA)
- Geochemistry & Mineralogy (AREA)
- Structural Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Processing Of Solid Wastes (AREA)
- Combustion & Propulsion (AREA)
- Civil Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
Abstract
A method using an alkaline process to extract alumina in coal ash relates to a method using coal ash to produce alumina and is characterized by comprising the steps of (1) manufacturing coal ash, limestone or lime into raw slurry with alkali liquid; (2) firing the raw slurry into clinker; (3) performing alkaline leaching on the clinker; (4) desiliconizing leaching liquid to perform liquid-solid separation; (5) carbonating and resolving desiliconized liquid after liquid-solid separation to obtain aluminium hydroxide; (6) roasting the aluminium hydroxide to achieve alumina; (7) performing alkaline leaching on solid phase residues obtained from the step (3); (8) using leaching liquid obtained from the step (7) to adjust molecular ratio of a system in desiliconization treatment; or adding lime in the leaching liquid obtained from the step (7), filtering after reaction, and obtaining filter residues which are used for desiliconization of the step (4). The method can be used for treating coal ash raw materials from different sources to produce alumina.
Description
Technical field
The present invention relates to a kind of alkaline process and extract method of alumina in the flyash.
Background technology
Flyash is the tiny powdered material of collecting the flue gas behind coal combustion.The mineralogical composition of flyash is relevant with the source of chemical ingredients and coal, and its thing phase composite is main with vitreum, contains the pulverulent material of mullite, quartz, rhombohedral iron ore, magnetite, anhydrite, tricalcium phosphate and melilith etc. simultaneously; Chemical ingredients is mainly Al
2O
3, SiO
2, Fe
2O
3, CaO, MgO etc., also contain a spot of rare elements simultaneously.Flyash is stored up and will be taken a large amount of soils, and also can cause pollution to a certain degree to surrounding enviroment.Therefore, the comprehensive utilization of flyash is studied, turned waste into wealth,, build environmental protection and saving type society and all be significant environment protection and raising resource utilization.
The technology of extracting aluminum oxide (white lake) or aluminium salt from flyash is concluded and can be divided into acid system, alkaline process and soda acid hybrid system.These process methodes respectively have its characteristics on operational path.
The acid system advantage is flyash staple SiO
2Do not get into solution, but shortcoming be to handle with aluminium altogether the impurity metallic elements of stripping need purifying treatment, the removal of impurities operation is tediously long, acid consumption is big and need acid-resistant system.The representative method of alkaline process is limestone sintering method and soda-lime sintering process.The flyash alkaline process extracts the aluminum oxide advantage and is that the metallic impurity interference is little, technology maturation.Alkaline process causes energy consumption too high because its clinker quantity is big, and becomes the quantity of slag big after the alumina extraction.
The flyash alkaline process extracts the solid slag that is produced in the alumina process can contain a certain amount of alkali and aluminum oxide.Effectively reducing alkali and alumina content in the solid slag, is to realize that the flyash alkaline process extracts the prerequisite of aluminum oxide maximization of economic benefit, the extensive recycling of realization solid slag.
Summary of the invention
The object of the invention is exactly the deficiency that exists to above-mentioned prior art; Provide a kind of explained hereafter flow process short; Alkaline consumption is low, and quality product is easy to control, can realize effectively extracting that the alkaline process of solid phase residue comprehensive utilization extracts method of alumina in the flyash behind the aluminum oxide.
The objective of the invention is to realize through following technical scheme.
A kind of alkaline process extracts method of alumina in the flyash, it is characterized in that the step of its leaching process comprises:
(1) in flyash, adds lime and alkali lye, process charge pulp;
(2) charge pulp is fired into grog;
(3) grog is carried out alkali and leach, leaching slurry is carried out liquid-solid separation, obtain solid phase residue 1 and leach liquor 1;
(4) leach liquor 1 is carried out desiliconization and handles after, carry out liquid-solid separation;
(5) with liquid after the desiliconization that filters to isolate, carry out carbonating and decompose, obtain white lake;
(6) white lake obtains alumina product after roasting;
(7) the solid phase residue 1 that obtains in the step (3) is carried out alkali again and leach, leaching slurry is carried out liquid-solid separation, obtain solid phase residue 2 and leach liquor 2, further reclaim aluminum oxide and alkali;
The molecular ratio of Adjustment System when the leach liquor 2 that (8) obtains in the step (7) is used for step (4) desiliconization processing; Add lime in the leach liquor that also can in step (7), obtain, the reaction after-filtration, the filter residue excessively that obtains is used for the desiliconization process of step (4);
(9) the solid phase residue 2 that obtains in the step (7) is as the raw material of material of construction such as production cement.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that the fineness of flyash in its step (1) is-0.18mm; The fineness of limestone powder or lime powder is-0.18mm.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that alkali lye that its step (1) adds is the mixed solution of the carbonating decomposition nut liquid after the evaporation of yellow soda ash and aluminum oxide production process.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that the mixing process of the charge pulp of its step (1), and the addition of Wingdale or lime is by SiO in the system
2Amount confirm that the addition of Wingdale or lime is according to CaO and SiO
2Mol ratio be 0.8～2.2 control, the yellow soda ash addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be 0.9～1.7 control.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, and the charge pulp firing temperature that it is characterized in that its step (2) is 900～1380 ℃, and the firing time is 10-120 minute.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that its step (3) is under the condition of 40～105 ℃ of temperature, to leach grog with adjustment liquid, and leaching slurry is carried out liquid-solid separation, obtains solid phase residue 1 and leach liquor 1.
A kind of flyash of the present invention is produced the method that aluminum oxide-alkali soaks the raw material that the alkali that reclaims in the solid slag and aluminum oxide-solid slag can be used as material of construction, and the leach liquor 1 that it is characterized in that its step (3) carries out carrying out after desiliconization is handled the some or all of step (1) of returning of solid residue that liquid-solid separation obtains and makes the raw material that charge pulp is prepared.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, and the mother liquor after the carbonating that it is characterized in that its step (5) is decomposed returns step (1) after evaporation, be used for the charge pulp preparation.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that it leaches the liquid-solid washing lotion allotment that separates back solid phase residue of slurries that adjustment liquid that grog uses who knows by leaching and forms.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that carrying out in its step (7) alkali and leaches the strength of solution of using and be NaO
2K30 ~ 250g/L, extraction temperature are 60 ~ 250 ℃, and extraction time is 5 ~ 360 minutes, and leaching liquid-solid ratio is 1 ~ 5, and leaching slurry is carried out liquid-solid separation, obtain solid phase residue 2 and leach liquor 2.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that the molecular ratio of Adjustment System when the leach liquor 2 that obtains in its step (7) is used for step (4) desiliconization.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, adds lime in the leach liquor 2 that it is characterized in that in step (7), obtaining, the reaction after-filtration, and the filter residue excessively that obtains is used for the desiliconization process of step (4);
A kind of alkaline process of the present invention extracts method of alumina in the flyash, it is characterized in that the solid phase residue 2 that obtains in its step (7) is used as the raw material of producing material of construction such as cement.
A kind of alkaline process of the present invention extracts method of alumina in the flyash, can be used for handling the powdered coal ash production aluminum oxide of different sources, different chemical composition and mineral composition, and alkali content is low in the solid slag; The raw material that can be used as material of construction, technology maturation of the present invention is reliable, compares with existing alkaline process production technique; Mass flow is little; The solid phase level of residue is few, and can realize the zero release of whole process, helps environment protection.Really realized flyash production full-range high yield of aluminum oxide and low energy expenditure, and the solid phase residue that extracts behind the aluminum oxide can be realized large-scale recycling fully.
Embodiment
A kind of alkaline process extracts method of alumina in the flyash; The step of its production process comprises: 1) that flyash is (levigate in case of necessity; Fineness is preferably-80 orders), limestone powder or lime powder (fineness is preferably-80 orders) after levigate, and the carbonating decomposition nut liquid after yellow soda ash and the evaporation is mixed and made into charge pulp according to a certain percentage; 2) charge pulp is fired into grog under certain temperature condition; 3) with the solution that contains yellow soda ash and sodium hydroxide etc. grog is leached under certain condition, leaching slurry is carried out liquid-solid separation; 4) leach liquor is carried out carrying out the carbonating decomposition again after the desiliconization, obtain white lake; 5) white lake obtains alumina product after roasting; 6) solid product that forms in the desiliconization process can return the raw material of charge pulp preparation stage as the preparation charge pulp; 7) mother liquor after carbonating is decomposed returns after evaporation, is used to prepare charge pulp; 8) leaching the liquid-solid washing lotion allotment that separates back solid phase residue of slurries that adjustment liquid that grog uses who knows by leaching forms; 9) with 3) in the solid phase residue that obtains carry out alkali again and leach, leaching slurry is carried out liquid-solid separation, further reclaim aluminum oxide and alkali; The leach liquor that obtains is used for 4) molecular ratio of Adjustment System when desiliconization is handled; Also can in the leach liquor that obtains, add lime, the reaction after-filtration, the filter residue of crossing that obtains is used for 4) desiliconization process; 10) the solid phase residue that finally obtains is as the raw material of material of construction such as production cement.
Embodiment 1
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
339%, SiO
244.1%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.0 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 1.1 control preparation charge pulies of preparing burden; Is to fire under 1110 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 69.97% in the grog, and the sodium oxide leaching yield can reach 70.46% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 50g/L is under 90 ℃ of conditions in temperature, leaches 360 minutes, and leaching liquid-solid ratio is 2, Al in the solid phase residue
2O
3Leaching yield be 15%, Na in the solid phase residue
2The leaching yield of O is 91%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 2
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
341%, SiO
247%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.3 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 1.0 control preparation charge pulies of preparing burden; Is to fire under 1200 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 77.76% in the grog, and the sodium oxide leaching yield can reach 82.78% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 100g/L is under 120 ℃ of conditions in temperature, leaches 20 minutes, and leaching liquid-solid ratio is 2, Al in the solid phase residue
2O
3Leaching yield be 16%, Na in the solid phase residue
2The leaching yield of O is 89%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 3
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
347%, SiO
243%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.5 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 1.2 control preparation charge pulies of preparing burden; Is to fire under 1120 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 84.97% in the grog, and the sodium oxide leaching yield can reach 92.82% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 140g/L is under 160 ℃ of conditions in temperature, leaches 15 minutes, and leaching liquid-solid ratio is 3, Al in the solid phase residue
2O
3Leaching yield be 17%, Na in the solid phase residue
2The leaching yield of O is 88%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 4
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
351%, SiO
238%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.4 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 1.05 control preparation charge pulies of preparing burden; Is to fire under 1250 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 84.17% in the grog, and the sodium oxide leaching yield can reach 88.21% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 200g/L is under 200 ℃ of conditions in temperature, leaches 10 minutes, and leaching liquid-solid ratio is 3, Al in the solid phase residue
2O
3Leaching yield be 18%, Na in the solid phase residue
2The leaching yield of O is 89%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 5
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
355%, SiO
237%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.6 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 1.0 control preparation charge pulies of preparing burden; Is to fire under 1150 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 86.21% in the grog, and the sodium oxide leaching yield can reach 94.12% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 200g/L is under 220 ℃ of conditions in temperature, leaches 8 minutes, and leaching liquid-solid ratio is 3, Al in the solid phase residue
2O
3Leaching yield be 18%, Na in the solid phase residue
2The leaching yield of O is 87%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 6
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
353%, SiO
238%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 1.5 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 0.98 control preparation charge pulp of preparing burden; Is to fire under 1230 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 84.46% in the grog, and the sodium oxide leaching yield can reach 92.78% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, control carbonating decomposition condition obtains the pseudo-boehmite product.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 70g/L is under 100 ℃ of conditions in temperature, leaches 240 minutes, and leaching liquid-solid ratio is 3, Al in the solid phase residue
2O
3Leaching yield be 13%, Na in the solid phase residue
2The leaching yield of O is 81%.The solid phase residue that finally obtains is as the raw material of producing cement.
Embodiment 7
Raw material is the flyash of certain heat power plant, and main chemical compositions is Al
2O
355%, SiO
237%, with grind the back fineness for the carbonating decomposition nut liquid after-80 order limestone powders or lime powder and yellow soda ash and the evaporation according to CaO and SiO
2Mol ratio be 2.05 controls, yellow soda ash (comprises the Na in the carbonating decomposition nut liquid after the evaporation
2O) addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be the 0.97 control preparation charge pulp of preparing burden; Is to fire under 1250 ℃ of conditions charge pulp in temperature, obtains qualified grog; Under 80-90 ℃ condition, leach grog with adjustment liquid, leaching rate of alumina can reach 88.21% in the grog, and the sodium oxide leaching yield can reach 96.16% in the grog.Clinker leaching liquor carries out carbonating and decomposes after desiliconization, obtain white lake, and white lake obtains the metallurgical-grade aluminum oxide product after roasting.
Solid phase residue after the grog stripping uses caustic sodium concentration to be NaO
2KThe alkali lye of 200g/L is under 220 ℃ of conditions in temperature, leaches 8 minutes, and leaching liquid-solid ratio is 3, Al in the solid phase residue
2O
3Leaching yield be 11%, Na in the solid phase residue
2The leaching yield of O is 81%.The solid phase residue that finally obtains is as the raw material of producing cement.
Claims (16)
1. an alkaline process extracts method of alumina in the flyash, it is characterized in that the step of its production process comprises:
(1) in flyash, adds lime and alkali lye, process charge pulp;
(2) charge pulp is fired into grog;
(3) grog is carried out alkali and leach, leaching slurry is carried out liquid-solid separation, obtain solid phase residue 1 and leach liquor 1;
(4) leach liquor 1 is carried out desiliconization and handles after, carry out liquid-solid separation;
(5) with liquid after the desiliconization that filters to isolate, carry out carbonating and decompose, obtain white lake;
(6) white lake obtains alumina product after roasting;
(7) the solid phase residue 1 that obtains in the step (3) is carried out alkali again and leach, leaching slurry is carried out liquid-solid separation, obtain solid phase residue 2 and leach liquor 2, further reclaim aluminum oxide and alkali;
The molecular ratio of Adjustment System when the leach liquor 2 that (8) obtains in the step (7) is used for step (4) desiliconization processing; Add lime in the leach liquor that also can in step (7), obtain, the reaction after-filtration, the filter residue excessively that obtains is used for the desiliconization process of step (4);
(9) the solid phase residue 2 that obtains in the step (7) is as the raw material of material of construction such as production cement.
2. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that the fineness of flyash in its step (1) is-0.18mm; The fineness of limestone powder or lime powder is-0.18mm.
3. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that the alkali lye that its step (1) adds is the mixed solution of the carbonating decomposition nut liquid after yellow soda ash and the evaporation.
4. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that the mixing process of the charge pulp of its step (1), and the addition of Wingdale or lime is by SiO in the system
2Amount confirm that the addition of Wingdale or lime is according to CaO and SiO
2Mol ratio be 0.8～2.2 control, the yellow soda ash addition is according to Na
2O and Al
2O
3+ Fe
2O
3Mol ratio be 0.9～1.7 control.
5. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, and the charge pulp firing temperature that it is characterized in that its step (2) is 900～1380 ℃, and the firing time is 10-120 minute.
6. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, and what it is characterized in that its step (3) is under the condition of 40～105 ℃ of temperature, to leach grog with adjustment liquid.
7. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that its step (4) obtains solid residue some or all ofly return the raw material that step (1) is done the charge pulp preparation.
8. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, and the mother liquor after the carbonating that it is characterized in that its step (5) is decomposed returns step (1) after evaporation, be used for the charge pulp preparation.
9. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that it leaches the liquid-solid washing lotion allotment that separates back solid phase residue of slurries that adjustment liquid that grog uses who knows by leaching and forms.
10. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that carrying out in its step (7) alkali and leaches the strength of solution of using and be NaO
2K30 ~ 250g/L.
11. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that carrying out in its step (7) extraction temperature that alkali leaches is 60 ~ 250 ℃.
12. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that carrying out in its step (7) extraction time that alkali leaches is 5 ~ 360 minutes.
13. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, it is characterized in that the liquid-solid ratio when carrying out alkali in its step (7) leaches is 1 ~ 5.
14. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash; It is characterized in that the molecular ratio of Adjustment System when the leach liquor 2 that obtains in its step (7) is used for step (4) desiliconization, the molecular ratio of desiliconization dope can be adjusted to 1.4 ~ 2.0.
15. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, adds lime in the leach liquor 2 that it is characterized in that in step (7), obtaining, the reaction after-filtration, and the filter residue excessively that obtains is used for the desiliconization process of step (4).
16. a kind of alkaline process according to claim 1 extracts method of alumina in the flyash, the solid phase residue 2 that it is characterized in that obtaining in its step (7) is as the raw material of producing material of construction.
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| CN201210084915.6A CN102627305B (en) | 2012-03-28 | 2012-03-28 | Method using alkaline process to extract alumina in coal ash |
| PCT/CN2012/087467 WO2013143335A1 (en) | 2012-03-28 | 2012-12-26 | Method for extracting aluminium oxide in fly ash by alkaline process |
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|---|---|---|---|
| CN201210084915.6A CN102627305B (en) | 2012-03-28 | 2012-03-28 | Method using alkaline process to extract alumina in coal ash |
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| CN103130254A (en) * | 2013-03-18 | 2013-06-05 | 中国铝业股份有限公司 | Method for producing aluminum oxide by using alkaline method |
| CN103130257A (en) * | 2013-03-18 | 2013-06-05 | 中国铝业股份有限公司 | Improved aluminum oxide production method |
| WO2013143335A1 (en) * | 2012-03-28 | 2013-10-03 | 中国铝业股份有限公司 | Method for extracting aluminium oxide in fly ash by alkaline process |
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| CN105776268A (en) * | 2016-02-06 | 2016-07-20 | 杭州锦江集团有限公司 | Drying firing method taking fly ash as raw material |
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Also Published As
| Publication number | Publication date |
|---|---|
| CN102627305B (en) | 2014-05-07 |
| WO2013143335A1 (en) | 2013-10-03 |
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