CN105692666A - Method for extracting alumina from high-alumina fly ash - Google Patents
Method for extracting alumina from high-alumina fly ash Download PDFInfo
- Publication number
- CN105692666A CN105692666A CN201610041350.1A CN201610041350A CN105692666A CN 105692666 A CN105692666 A CN 105692666A CN 201610041350 A CN201610041350 A CN 201610041350A CN 105692666 A CN105692666 A CN 105692666A
- Authority
- CN
- China
- Prior art keywords
- dissolution
- mixed
- ash
- calcium silicate
- solid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- C01F7/062—Digestion
-
- 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
- C01F7/066—Treatment of the separated residue
-
- 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
Abstract
The invention provides a method for extracting alumina from high-alumina fly ash. The method comprises the following steps of mixing the high-alumina fly ash with alkali liquor and performing first dissolution treatment, wherein the temperature is 200 to 270DEG C, the concentration of the alkali liquor is 200 to 300g/l, and the solid content of a mixed solution is 150 to 400g/l; performing solid-liquid separation on the mixed solution obtained by the first dissolution treatment to obtain primary calcium silicate slags and a first dissolution solution; mixing the primary calcium silicate slags with limestone to obtain a mixing material with the alkali ratio of 0.90 to 0.98 and the calcium ratio of 1.4 to 1.9; calcining the mixing material, mixing the calcined mixing material with dissolution adjusting liquid, and performing second dissolution treatment; performing solid-liquid separation on a mixed solution obtained by the second dissolution treatment to obtain calcium silicate slags and a second dissolution solution; mixing the first dissolution solution with the second dissolution solution, and performing seed decomposition, carbonation decomposition treatment and calcination to obtain alumina. According to the method provided by the invention, the flow of system materials is reduced, and energy consumption is reduced; meanwhile, the method is simple and convenient in operation, and the quantity of the slags is small.
Description
Technical field
The present invention relates to a kind of method that aluminous fly-ash extracts aluminium oxide, belong to resource regeneration technical field。
Background technology
Aluminous fly-ash is the alumina resource that China is potential, and in recent years, Duo Jia R&D institution and enterprise extract aluminium oxide for aluminous fly-ash and carried out tackling of key scientific and technical problems and Industrialization, and comparatively ripe is adopt pre-desiliconizing-soda lime sintering process at present。Inner Mongol a company utilizes the Showcase Production Line that aluminous fly-ash produces 240000 tons of aluminium oxidies per year to have been put into running, and current operation conditions just tends towards stability。But the technological requirement according to pre-desiliconizing-soda lime sintering process, the desiliconization flyash utilizing alumina silica ratio to be 2.0 produces 1 ton of aluminium oxide, take around the limestone consuming about 3.5 tons, if large-scale production, initiation limestone is dug up mine, transport, store up and the many difficulties such as the silico-calcium quantity of slag is excessive。
Recent years, the research extracting aluminium oxide about low alumina-silica ratio mineral launches more, the such as patent No. is CN102249253A, denomination of invention is " aluminous fly-ash produces the method for aluminum and coproducing active calcium silicate " and the patent No. patent that to be CN101966999A, denomination of invention be " method of aluminous fly-ash two step alkali solution technique extraction aluminium oxide and white carbon ", it it is all the thinking adopting firstly extracting silicon and secondly extracting aluminum, improve element to utilize, but both energy consumptions are high, the quantity of slag is big, and particularly the efficiency extracting aluminium oxide of the latter is low；The patent No. has been the patent Introduction of " method of producing alumina through series process " of CN101928025A, and bauxite Bayer process dissolution is obtained aluminum silicon weight ratio is the Bayer process red mud of 1.0～2.0, adds sodium carbonate, limestone or lime sintering and obtain sintered clinker in Bayer process red mud；Sintering process dissolution serosity is mixed with bayer process ' s digested slurry and is diluted and then desiliconization obtains aluminium oxide。Using the method must add sodium carbonate in Bayer process red mud, simultaneously two kinds of ore pulp mixing, mass flow is bigger。
In sum, there is the problems such as energy consumption height, the quantity of slag is big, feed proportioning is loaded down with trivial details in current China flyash extraction aluminum oxide technology。
Summary of the invention
For the problems of the prior art, the present invention provides a kind of method that aluminous fly-ash extracts aluminium oxide, and to realize reducing energy consumption, reducing quantity of slag discharge, operation is simple simultaneously。
For achieving the above object, on the one hand, the present invention provide a kind of aluminous fly-ash extract aluminium oxide method, including:
Step A, aluminous fly-ash and alkali liquor being mixed and carry out the first dissolution process, temperature is 200-270 DEG C, and concentration of lye is 200-300g/l, mixed liquor solid content is 150-400g/l, described first dissolution is processed the mixed liquor solid-liquid separation obtained and obtains primary calcium silicate slag and the first dissolution fluid；
Step B, described primary calcium silicate slag is mixed acquisition alkali than 0.90-0.98, the calcium compound than 1.4-1.9 with limestone, adjust liquid mixing carry out the second dissolution process with dissolution after described compound is calcined, described second dissolution is processed the mixed liquor solid-liquid separation obtained and obtains calcium silicate slag and the second dissolution fluid；
Step C, mixes described first dissolution fluid and the second dissolution fluid, obtains aluminium oxide after carrying out kind point and carbon divisional processing and being fired。
In method provided by the invention, at twice the aluminium oxide in aluminous fly-ash is carried out dissolution extraction, being made directly the first dissolution reaction first with aluminous fly-ash and lye solution, the alumina extraction by therein about 50% out, reduces follow-up system mass flow；Calcine after the primary calcium silicate slag containing residue aluminium oxide is added limestone, be substantially reduced the energy consumption of rotary kiln。In the method, twice dissolution feed proportioning is simple, extracts the in hgher efficiency of aluminium oxide than traditional low alumina-silica ratio Bayer process with sintering process, and the quantity of slag is lower, has obvious Social benefit and economic benefit, therefore has good Industry Promotion and is worth。
In method provided by the invention, in aluminous fly-ash, alumina content is not less than 43%。The kind of alkali liquor does not limit, can and SiO2And Al2O3Reaction generates soluble aluminum hydrochlorate and silicate, and sodium hydroxide generally can be used as alkali liquor。
In step A, the reaction that the first dissolution occurs in processing is:
SiO2+ 2NaOH=Na2SiO3+H2O(1)
Al2O3+ 2NaOH=2NaAlO2+H2O(2)
According to formula (2), alkali liquor further can not generate reaction stopping during sodium aluminate by dissolution aluminium oxide, and the time of process is determined by response situation, is generally 0.5-5 hour。After the first dissolution processes, it is possible to by part alumina extraction in aluminous fly-ash out, the reacted sodium aluminate that is converted into enters in the first dissolution fluid, and remaining aluminium oxide need to carry out further dissolution by subsequent step。
In one embodiment of the invention, aluminous fly-ash and alkali liquor being mixed before carrying out the first dissolution process, may also include use alkali liquor and described aluminous fly-ash is carried out pre-desiliconizing process, condition is temperature 65-80 DEG C, concentration of lye is 80-100g/l, and the process time is 2-4 hour。To deviate from amorphous Si O in aluminous fly-ash in advance2, reduce mass flow, improve alumina silica ratio。
In step B, the first dissolution is calcined after processing the primary calcium silicate slag obtained and limestone mixing, and calcination condition processes 0.5-3 hour at being generally 1000-1300 DEG C。Shown in the reaction such as formula (3) occurred in this calcination process, the grog of generation mainly contains the thing phases such as dicalcium silicate, sodium aluminate。
Ca2CO3+Na2O·Al2O3·2SiO2=2CaO SiO2+Na2O·Al2O3+CO2(3)
Using dissolution to adjust liquid in step B further and grog carries out the second dissolution process, it is for carrying out the conventional substances of alumina extraction in this area that dissolution adjusts liquid, is generally the solution comprising certain density aluminium oxide, sodium oxide and sodium carbonate。The dissolution used in the present invention adjusts causticization coefficient (i.e. molecular proportion, the Na of liquid2O and A12O3Mol ratio) for 1.3-1.5, concentration of sodium carbonate is 13-15g/l。The condition that second dissolution processes be at liquid-solid ratio 3:1, processes 0.5-1.0 hour at temperature 60-85 DEG C, and what be more beneficial in grog aluminium oxide effectively extracts。After this second dissolution processes, the most of aluminium oxide in primary calcium silicate slag is extracted, and is converted into sodium aluminate and enters in the second dissolution fluid。So far, in aluminous fly-ash raw material, the aluminium oxide of 80-90% can be extracted by twice dissolution process of the present invention。
In this step A and step B, solid-liquid separation adopts filter press or other conventional filtering equipment, primary calcium silicate slag and limestone mixing device therefor to be ball mill, and calciner is rotary kiln。The water content control of the primary calcium silicate slag obtained after the first dissolution processes is about 40-50%, and water content is relatively low, and therefore the feeding manner of rotary kiln can adopt semidry method feeding。
In step C, after described first dissolution fluid and the second dissolution fluid being mixed, also including being mixed liquid heating and to 160-180 DEG C and be incubated 0.5-2 hour, the desiliconization carrying out dissolution fluid processes。
Generally described first dissolution fluid and the second dissolution fluid can be mixed according to volume ratio 1:1-2, it is thus achieved that the mixed liquor that alkali concn is relatively low, be conducive to the carrying out of follow-up desiliconization step。According to known technology industrial at present, the mixed liquor of the first dissolution fluid and the second dissolution fluid can be processed through two sections of deep desilications, finally obtain aluminium oxide then through roasting after seeded precipitation and carbonation decomposition。
Such as, two sections of deep desilications process shown in course of reaction such as formula (4)-(6)。
One section of desiliconization:
1.7Na2SiO3+2NaAl(OH)4=Na2O·Al2O3·1.7SiO2·nH2O+3.4NaOH(4)
Two-stage desilication:
3Ca(OH)2+2NaAl(OH)4=3CaO Al2O3·6H2O+2NaOH(5)
3CaO·Al2O3·6H2O+xNa2SiO3=3CaO Al2O3·xSiO2·(6-2x)H2O+2xNaOH(6)
Above-mentioned two sections of deep desilications process such as can adopt following methods: one section of deep desilication stops more than 1h after being heated to 150-160 DEG C so that it is in most of SiO2Precipitating out with hydrated aluminum silicate form, be then fed in subsider and carry out solid-liquid separation, underflow solid after filtering is delivered to raw material preparation section and is prepared raw slurry, and the 35% of overflow obtains desiliconization seminal fluid after leaf filter is refining, is sent to decomposition process and carries out seeded precipitation。Add lime cream at all the other one section of desiliconization liquids of 65% and carry out two-stage nitration deep desilication so that it is in SiO2Precipitating out with calcium aluminosilicate hydrate form, be then fed in subsider and carry out solid-liquid separation, raw material preparation section raw slurry delivered to by underflow solid after filtering, overflow after leaf filter is refining desiliconization seminal fluid is sent to decomposition process and carries out carbonation decomposition。
In said method provided by the invention, after also including the mixed liquor solid-liquid separation described first dissolution process obtained, wash the first filter cake and obtain primary calcium silicate slag；After described second dissolution is processed the mixed liquor solid-liquid separation obtained, wash the second filter cake and obtain calcium silicate slag。
By washing the first filter cake and the second filter cake, alkali liquor therein can be removed, except improving the purity of primary calcium silicate slag and calcium silicate slag, also help recycle of alkali liquor。Such as in one embodiment, can the washing liquid that wash acquisition described in twice being mixed, adjusting its concentration is 200-340g/l, uses as described alkali liquor。
The enforcement of the present invention program, at least has the advantage that
1, in method provided by the invention, at twice the aluminium oxide in aluminous fly-ash is carried out dissolution extraction, reduce system mass flow；Calcining step can use semidry method feeding, is substantially reduced the energy consumption of rotary kiln。
2, in method provided by the invention, first dissolution process and the second dissolution mixing processing simply, easily operate, and the aluminium oxide of 80-95% in aluminous fly-ash raw material can be extracted, the in hgher efficiency of aluminium oxide is extracted with sintering process than traditional low alumina-silica ratio Bayer process, the quantity of slag is lower, there is obvious Social benefit and economic benefit, therefore there is good Industry Promotion and be worth。
Accompanying drawing explanation
Fig. 1 is the process chart of the inventive method。
Detailed description of the invention
For making the object, technical solutions and advantages of the present invention clearly, below in conjunction with accompanying drawing, the technical scheme in the embodiment of the present invention is clearly and completely described, it is clear that, described embodiment is a part of embodiment of the present invention, rather than whole embodiments。Based on the embodiment in the present invention, the every other embodiment that those of ordinary skill in the art obtain under not making creative work premise, broadly fall into the scope of protection of the invention。
Embodiment one
As shown in table 1, its alumina content is 48.75% to the aluminous fly-ash composition that the present embodiment adopts。Thing phase composition main in aluminous fly-ash is mullite, corundum, amorphous SO2Deng。
Table 1
The present embodiment adopts flow process as shown in Figure 1 to extract aluminium oxide:
It is that 80g/l sodium hydroxide solution is mixed and heated to 80 DEG C of pre-desiliconizings 2 hours by the aluminous fly-ash of alumina content 48.75% and concentration, aluminous fly-ash after pre-desiliconizing and sodium hydroxide solution that concentration is 200g/l being configured to serosity that solid content is 150g/l and pours into after stirring in autoclave, at 200 DEG C, dissolution carries out the first dissolution process for 5 hours。
Described first dissolution enters filter press solid-liquid separation after processing the mixed liquor cooling obtained, it is thus achieved that the first dissolution fluid and the first filter cake, washes this first filter cake with water and obtains primary calcium silicate slag。Primary calcium silicate slag enters ball mill and limestone mixing, and after mixing, material alkali ratio is 0.90, and calcium ratio is 1.4, and material enters rotary kiln through belt transport and calcines, condition be 1000-1300 DEG C at calcination processing 0.5-3 hour, it is thus achieved that grog。Using dissolution to adjust liquid after clinker cooling and it is carried out the second dissolution process, dissolution adjusts the causticization coefficient 1.3-1.5 of liquid, and sodium carbonate liquor concentration is 13-15g/L。The condition that second dissolution processes is for being 3:1 in liquid-solid ratio, processing 0.5-1.0 hour at temperature 60-85 DEG C。After the mixed liquor cooling after process, enter filter press solid-liquid separation, it is thus achieved that the second dissolution fluid and the second filter cake, wash this second filter cake with water and obtain calcium silicate slag。
It is that 1:1 collaborates by the first dissolution fluid and the second dissolution fluid according to volume ratio, being heated to 160 DEG C afterwards and be incubated 2 hours, two sections of deep desilications obtain desiliconization seminal fluid after processing, and desiliconization seminal fluid carries out the kind of routine and divides and divide with carbon, obtaining aluminium hydroxide, roasting obtains aluminium oxide。
Above-mentioned two sections of deep desilications process such as can adopt following methods: one section of deep desilication be heated to 160 DEG C after insulation 2 hours so that it is in most of SiO2Precipitating out with hydrated aluminum silicate form, be then fed in subsider and carry out solid-liquid separation, underflow solid after filtering is delivered to raw material preparation section and is prepared raw slurry, and the 35% of overflow obtains desiliconization seminal fluid after leaf filter is refining, is sent to decomposition process and carries out seeded precipitation。Add lime cream at all the other one section of desiliconization liquids of 65% and carry out two-stage nitration deep desilication so that it is in SiO2Precipitating out with calcium aluminosilicate hydrate form, be then fed in subsider and carry out solid-liquid separation, raw material preparation section raw slurry delivered to by underflow solid after filtering, overflow after leaf filter is refining desiliconization seminal fluid is sent to decomposition process and carries out carbonation decomposition。
To wash the washing liquid mixing of acquisition described in twice, washing liquid weight is in the first filter cake and the second filter cake 2 times of total butt weight, and evaporation, to adjust its concentration for 200g/l, enters pre-desiliconizing and the use of the first dissolution treatment process as described alkali liquor。
Aluminium oxide in aluminous fly-ash is carried out dissolution extraction by method that this embodiment provides at twice, and total extraction rate reached of aluminium oxide, to 90%, reduces system mass flow simultaneously。Primary calcium silicate slag is calcined after adding limestone, owing to material water ratio is low, it may be achieved semidry method feeding, is substantially reduced the energy consumption of rotary kiln, and the sodium hydroxide in the method achieves and recycles simultaneously。Twice dissolution feed proportioning is simple, extracts the in hgher efficiency of aluminium oxide than traditional low alumina-silica ratio Bayer process with sintering process, and the quantity of slag is lower, has obvious Social benefit and economic benefit, therefore has good Industry Promotion and is worth。
Embodiment two
The present embodiment adopts the powdered coal ash identical with embodiment one, and adopts flow process as shown in Figure 1 to extract aluminium oxide:
It is that 90g/l sodium hydroxide solution is mixed and heated to 70 DEG C of pre-desiliconizings 3 hours by the aluminous fly-ash of alumina content 48.75% and concentration, aluminous fly-ash after pre-desiliconizing and sodium hydroxide solution that concentration is 230g/l being configured to serosity that solid content is 300g/l and pours into after stirring in autoclave, at 250 DEG C, dissolution carries out the first dissolution process for 2.5 hours。
Described first dissolution enters filter press solid-liquid separation after processing the mixed liquor cooling obtained, obtain the first dissolution fluid and the first filter cake, wash this first filter cake with water and obtain primary calcium silicate slag, primary calcium silicate slag enters ball mill and limestone mixing, after mixing, material alkali ratio is 0.94, and calcium ratio is 1.7, and material enters rotary kiln through belt transport and calcines, condition processes 0.5-3 hour at being 1000-1300 DEG C, it is thus achieved that grog。Using dissolution to adjust liquid after clinker cooling and it is carried out the second dissolution process, it is 1.3-1.5 that dissolution adjusts the causticization coefficient of liquid, and sodium carbonate liquor concentration is 13-15g/L。The condition that second dissolution processes is for being 3:1 in liquid-solid ratio, processing 0.5-1.0 hour at temperature 60-85 DEG C。After the mixed liquor cooling after process, enter filter press solid-liquid separation, it is thus achieved that the second dissolution fluid and the second filter cake, wash this second filter cake with water and obtain calcium silicate slag。
It is that 1:1.5 collaborates by the first dissolution fluid and the second dissolution fluid according to volume ratio, being heated to 170 DEG C afterwards and be incubated 1 hour, obtain desiliconization seminal fluid after adopting the method desiliconization in embodiment 1, desiliconization seminal fluid carries out the kind of routine and divides and divide with carbon, obtaining aluminium hydroxide, roasting obtains aluminium oxide。
To wash the washing liquid mixing of acquisition described in twice, washing liquid is in the first filter cake and the second filter cake 2.5 times of total butt weight, and evaporation, to adjust its concentration for 300g/l, enters pre-desiliconizing and the use of the first dissolution treatment process as described alkali liquor。
Compared with embodiment 1, the sodium hydroxide solution employing higher concentration in the present embodiment also improves accordingly as alkali liquor, mixed liquor solid content and the first dissolution treatment temperature, thus shortening the time that the first dissolution processes, total extraction rate reached of aluminium oxide is to 92%；Alkali improves than with calcium ratio simultaneously, makes grog porosity and looseness, it is simple to the dissolution of the aluminium oxide in grog when the second dissolution processes。
Embodiment three
The present embodiment adopts the powdered coal ash identical with embodiment one, and adopts flow process as shown in Figure 1 to extract aluminium oxide:
It is that 100g/l sodium hydroxide solution is mixed and heated to 65 DEG C of pre-desiliconizings 4 hours by the aluminous fly-ash of alumina content 48.75% and concentration, aluminous fly-ash after pre-desiliconizing and sodium hydroxide solution that concentration is 270g/l being configured to serosity that solid content is 400g/l and pours into after stirring in autoclave, at 270 DEG C, dissolution carries out the first dissolution process for 0.5 hour。
Described first dissolution enters filter press solid-liquid separation after processing the mixed liquor cooling obtained, obtain the first dissolution fluid and the first filter cake, wash this first filter cake with water and obtain primary calcium silicate slag, primary calcium silicate slag enters ball mill and limestone mixing, after mixing, material alkali ratio is 0.98, and calcium ratio is 1.9, and material enters rotary kiln through belt transport and calcines, condition processes 0.5-3 hour at being 1000-1300 DEG C, it is thus achieved that grog。Using dissolution to adjust liquid after clinker cooling and it is carried out the second dissolution process, it is 1.3-1.5 that dissolution adjusts the causticization coefficient of liquid, and sodium carbonate liquor concentration is 13-15g/L。The condition that second dissolution processes is for being 3:1 in liquid-solid ratio, processing 0.5-1 hour at temperature 60-85 DEG C。After the mixed liquor cooling after process, enter filter press solid-liquid separation, it is thus achieved that the second dissolution fluid and the second filter cake, wash this second filter cake with water and obtain calcium silicate slag。
It is that 1:2 collaborates by the first dissolution fluid and the second dissolution fluid according to volume ratio, being heated to 180 DEG C afterwards and be incubated 2 hours, obtain desiliconization seminal fluid after adopting the method desiliconization in embodiment 1, desiliconization seminal fluid carries out the kind of routine and divides and divide with carbon, obtaining aluminium hydroxide, roasting obtains aluminium oxide。
To wash the washing liquid mixing of acquisition described in twice, washing liquid is in the first filter cake and the second filter cake 3 times of total butt weight, and evaporation, to adjust its concentration for 340g/l, enters pre-desiliconizing and the use of the first dissolution treatment process as described alkali liquor。
The present embodiment further increases the concentration of sodium hydroxide solution and the temperature of dissolution process, shortens the time that the first dissolution processes, and total extraction rate reached of aluminium oxide is to 95%；Alkali improves than further than with calcium simultaneously, the dissolution of the aluminium oxide in grog when being conducive to the second dissolution to process。
Last it is noted that various embodiments above is only in order to illustrate technical scheme, it is not intended to limit；Although the present invention being described in detail with reference to foregoing embodiments, it will be understood by those within the art that: the technical scheme described in foregoing embodiments still can be modified by it, or wherein some or all of technical characteristic is carried out equivalent replacement；And these amendments or replacement, do not make the essence of appropriate technical solution depart from the scope of various embodiments of the present invention technical scheme。
Claims (10)
1. the method that an aluminous fly-ash extracts aluminium oxide, it is characterised in that including:
Aluminous fly-ash and alkali liquor are mixed and carries out the first dissolution process, temperature is 200-270 DEG C, concentration of lye is 200-300g/l, aluminous fly-ash and alkali liquor are mixed the mixed liquor solid content obtained is 150-400g/l, and the mixed liquor solid-liquid separation after described first dissolution being processed obtains primary calcium silicate slag and the first dissolution fluid；
Described primary calcium silicate slag is mixed acquisition alkali than 0.90-0.98, the calcium compound than 1.4-1.9 with limestone, adjust liquid mixing carry out the second dissolution process with dissolution after described compound is calcined, described second dissolution is processed the mixed liquor solid-liquid separation obtained and obtains calcium silicate slag and the second dissolution fluid；
Described first dissolution fluid and the second dissolution fluid are mixed, after carrying out seeded precipitation and carbonation decomposition process and being fired, obtains aluminium oxide。
2. method according to claim 1, it is characterised in that the described first dissolution process time is 0.5-5 hour。
3. method according to claim 1, it is characterised in that to 160-180 DEG C and described first dissolution fluid and the second dissolution fluid mixing post-heating are incubated 0.5-2 hour, obtains aluminium oxide after carrying out seeded precipitation and carbonation decomposition process and being fired。
4. method according to claim 1, it is characterised in that second dissolution process condition for liquid-solid ratio be at 3:1,60-85 DEG C process 0.5-1.0 hour。
5. method according to claim 4, it is characterised in that it is 1.3-1.5 that described dissolution adjusts the causticization coefficient of liquid, and concentration of sodium carbonate is 13-15g/l。
6. method according to claim 1, it is characterised in that described first dissolution fluid and the second dissolution fluid are mixed according to volume ratio 1:1-2。
7. method according to claim 1, it is characterised in that the water content making described primary calcium silicate slag is 40-50%。
8. the method according to any one of claim 1-7, it is characterized in that, aluminous fly-ash and alkali liquor are mixed before carrying out the first dissolution process, also include using alkali liquor that described aluminous fly-ash is carried out pre-desiliconizing process, pre-desiliconizing treatment temperature 65-80 DEG C, concentration of lye is 80-100g/l, and the process time is 2-4 hour。
9. the method according to any one of claim 1-7, it is characterised in that after also including the mixed liquor solid-liquid separation described first dissolution process obtained, wash the first filter cake and obtain primary calcium silicate slag；After described second dissolution is processed the mixed liquor solid-liquid separation obtained, washing the second filter cake and obtain calcium silicate slag, the washing liquid washing acquisition mixed described in twice, adjusting its concentration is 200-340g/l, uses as described alkali liquor。
10. the method according to any one of claim 1-7, it is characterised in that in aluminous fly-ash, alumina content is not less than 43%。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610041350.1A CN105692666B (en) | 2016-01-20 | 2016-01-20 | A kind of method of aluminous fly-ash extraction aluminum oxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610041350.1A CN105692666B (en) | 2016-01-20 | 2016-01-20 | A kind of method of aluminous fly-ash extraction aluminum oxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105692666A true CN105692666A (en) | 2016-06-22 |
| CN105692666B CN105692666B (en) | 2017-12-12 |
Family
ID=56228384
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610041350.1A Expired - Fee Related CN105692666B (en) | 2016-01-20 | 2016-01-20 | A kind of method of aluminous fly-ash extraction aluminum oxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105692666B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055582A (en) * | 2016-12-15 | 2017-08-18 | 中国恩菲工程技术有限公司 | The system of Aluminum from flyash |
| CN108455638A (en) * | 2018-01-25 | 2018-08-28 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A method of producing aluminum and coproducing 4A zeolite molecular sieves |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242313A (en) * | 1980-03-21 | 1980-12-30 | Extraction Research & Development, Inc. | Processes for the recovery of alumina from fly ash and production of cement constituents |
| CN101759212A (en) * | 2010-01-08 | 2010-06-30 | 朔州市润泽投资发展有限公司 | Method for extracting aluminum oxide from sodium-free desiliconized fly ash |
| CN101966999A (en) * | 2010-11-11 | 2011-02-09 | 中国地质大学（北京） | Method for extracting aluminum oxide and white carbon black through two-step alkaline leaching method by adopting high-alumina fly ash |
| US20130343971A1 (en) * | 2011-05-11 | 2013-12-26 | Inner Mongolia Datang International Recycling Resource Development Co., Ltd. | Method for co-producing alumina and activated calcium silicate from high-alumina fly ash |
| CN104030331A (en) * | 2014-06-27 | 2014-09-10 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | Method for producing aluminum oxide by utilizing high-alumina fly ash |
-
2016
- 2016-01-20 CN CN201610041350.1A patent/CN105692666B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4242313A (en) * | 1980-03-21 | 1980-12-30 | Extraction Research & Development, Inc. | Processes for the recovery of alumina from fly ash and production of cement constituents |
| CN101759212A (en) * | 2010-01-08 | 2010-06-30 | 朔州市润泽投资发展有限公司 | Method for extracting aluminum oxide from sodium-free desiliconized fly ash |
| CN101966999A (en) * | 2010-11-11 | 2011-02-09 | 中国地质大学（北京） | Method for extracting aluminum oxide and white carbon black through two-step alkaline leaching method by adopting high-alumina fly ash |
| US20130343971A1 (en) * | 2011-05-11 | 2013-12-26 | Inner Mongolia Datang International Recycling Resource Development Co., Ltd. | Method for co-producing alumina and activated calcium silicate from high-alumina fly ash |
| CN104030331A (en) * | 2014-06-27 | 2014-09-10 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | Method for producing aluminum oxide by utilizing high-alumina fly ash |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055582A (en) * | 2016-12-15 | 2017-08-18 | 中国恩菲工程技术有限公司 | The system of Aluminum from flyash |
| CN107055582B (en) * | 2016-12-15 | 2021-10-22 | 中国恩菲工程技术有限公司 | System for dissolve out aluminium from fly ash |
| CN108455638A (en) * | 2018-01-25 | 2018-08-28 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A method of producing aluminum and coproducing 4A zeolite molecular sieves |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105692666B (en) | 2017-12-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2014392419B2 (en) | Method for recycling alkali and aluminum during treatment of Bayer red mud by using calcification-carbonization process | |
| CN101928025B (en) | Method for producing alumina through series process | |
| CN104386720B (en) | Method for acid-alkali combined extraction of alumina from high-silicon aluminum-containing mineral raw material | |
| CN101746795B (en) | Method for producing alumina from bauxite | |
| Miller et al. | Alumina production by the pedersen process—History and future | |
| WO2018233688A1 (en) | Method for preparing aluminum hydroxide by treating medium- and low-grade bauxite by using one-step alkali heat process of andradite | |
| CN109279633A (en) | A kind of method of low-temperature bake bauxite production aluminium hydroxide | |
| CN1296280C (en) | Method for combination producing alumina and cement from chalk and flyash | |
| CN103950960B (en) | A kind of method of producing aluminum oxide without evaporation based on calcification-carborization | |
| CN103936046B (en) | The method of ore deposit calcification transition is added after in a kind of aluminum oxide production process | |
| CN102583475B (en) | Method for producing aluminum oxide by utilizing low alumina-silica ratio aluminized resource dry method or semidry method | |
| CN105692666B (en) | A kind of method of aluminous fly-ash extraction aluminum oxide | |
| CN103332711A (en) | Deep desilicication method of high-alumina fly ash | |
| CN100593018C (en) | Technological process method of producing aluminium oxide using high aluminium slag | |
| US4512809A (en) | Process for producing, from aluminous siliceous materials, clinker containing alkali metal aluminate and dicalcium silicate, and use thereof | |
| CN110217811A (en) | A kind of series process process for making alumina | |
| CN105753025B (en) | The method that aluminum oxide is produced using aluminous fly-ash | |
| RU2360865C1 (en) | Processing method of bauxites on alumina | |
| CN101870484B (en) | Process for producing aluminium hydroxide and cement by utilizing fly ash | |
| CN101870485B (en) | Process for producing aluminium hydroxide and cement by utilizing high silicon low aluminium raw mineral materials | |
| CN103964478B (en) | The method of a kind of calcification-carborization process middle-low grade aluminum-containing raw material and aluminium circulation | |
| CN101870487B (en) | Process for producing aluminium hydroxide and cement by utilizing fly ash | |
| CN107935005B (en) | Method for pretreating fly ash carbonate solution and extracting alumina | |
| CN101870483B (en) | Process for producing aluminium hydroxide and cement by utilizing gangue | |
| CN104119009B (en) | Calcium silicate slag is as the purposes of clinker sintering aid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20171212 Termination date: 20210120 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |