CN101306926A - Process for abstracting floating air ball from fly ash or slag - Google Patents
Process for abstracting floating air ball from fly ash or slag Download PDFInfo
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- CN101306926A CN101306926A CNA2008101153564A CN200810115356A CN101306926A CN 101306926 A CN101306926 A CN 101306926A CN A2008101153564 A CNA2008101153564 A CN A2008101153564A CN 200810115356 A CN200810115356 A CN 200810115356A CN 101306926 A CN101306926 A CN 101306926A
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Abstract
The invention relates to a method for comprehensively utilizing fly ash and furnace cinder, in particularly to a method for extracting floating beads from the fly ash or the furnace cinder. The method comprises the following: a working procedure of screening refined iron sand from the fly ash or the furnace cinder; a working procedure of flotating floating beads; a working procedure of pre-desiliconization; a technological flow of producing white carbon black; a technological flow of producing aluminum oxide; and a technological flow of producing cement by utilization of waste residue. The method arranges a flotating device before pre-desiliconization technological reaction to extract the floating beads from the reacted mixture, and can obtain white floating bead products after decarbonization and secondary selection. Simultaneously, the white carbon black, the aluminum oxide and the joint cement can be organically, continuously and sequentially extracted from the fly ash or the furnace cinder after the floating beads are extracted, thereby the method realizes comprehensive utilization of the fly ash or the furnace cinder.
Description
[technical field]
The present invention relates to the resource utilization method of a kind of flyash or slag, relate in particular to a kind of method of floating pearl of from flyash or slag, extracting.
[background technology]
The bulk deposition of firepower electrical plant discharging flyash has caused serious pollution to surrounding environment.Floating pearl and be a kind of composition in the flyash, account for 5～10% of flyash total amount, have light weight, insulation, multifrequency nature such as corrosion-resistant, should be one of important channel of total utilization of PCA as the stopping composition of matrix material.Thisly float pearl and in building materials, thermal control material, chemical industry, important use is arranged, can be used as the polymkeric substance stopping composition as it.
In recent years, most of achievement in research of extracting useful resources both at home and abroad from flyash or slag only has theory significance, the major cause that limits these achievement in research industrialization is that not system is studied in the extraction of flyash or slag useful resources, for example, some is research extraction aluminum oxide separately, some specialize in the extraction silicon oxide, some special ferric oxide that extracts, some specialize in extraction carbon, and other are specialized in and extract trace element, and these researchs are all established one's own system, do not carry out the extraction of resource interrelated, integrate, and make it to become a feasible overall plan, and make extraction cost high, be difficult to carry out Industry Promotion.
[summary of the invention]
Given this, this patent proposes a kind of method, and purpose is to add a flotation unit before pre-desilication process reaction, will float pearl and extract from the mixture of reaction, and through de-carbon, recleaning can obtain white products and float pearl.
For achieving the above object, the invention provides a kind of from from flyash or slag, extracting the method float pearl, comprising following steps:
Step 1: slag is ground, from dry powder coal ash or slag, magneticly elect smart iron sand after, stir after adding sodium hydroxide solution;
Step 2: after treating to float floating matter on the liquid level, the unlatching floatation equipment will float to be collected in the dashpot after pearl is chosen;
Step 3:, and just can obtain the white pearl product that floats through sorting once more, washing through the de-carbon operation.
Further, in step 1, the concentration of described sodium hydroxide solution and amount are: mass percent is 10%～40% NaOH solution, and according to solid-to-liquid ratio: i.e. flyash or slag quality (kilogram) and pre-desiliconization is to carry out proportioning in 1: 1.6～1: 8 with the volume ratio (liter) of sodium hydroxide solution.
Further, in step 1, the processing condition of described stirring are: normal temperature starts whipping device down, and rotating speed keeps rotating 2～10 minutes at 20～50 rev/mins.
Further, the method for flyash or slag coproduction ferric oxide is, in step 1:
At first with agitating ball mill with slag mesh-of-grind to 200～250 orders;
Slag after flyash or the grinding carries out magnetic separation with dry-type magnetic extractor, and magneticstrength is 1100～1300 oersteds, just can obtain the crude iron washed ore;
The crude iron washed ore is through taking off the magnetic machine demagnetization;
Pass through the one-level magnetic plant again, magneticstrength is 900～1050 oersteds, carries out can obtaining smart iron sand after the magnetic separation.
Further, flyash or slag coproduction method of alumina are that after pearl was floated in extraction, flyash or slag carried out following steps with the slurries of sodium hydroxide solution:
Steps A: pre-desiliconization: the concentration and the amount that add sodium hydroxide solution in flyash or the slag are, mass percent is between 10%～40%, is to carry out proportioning in 1: 1.6～1: 8 according to the quality (kilogram) of flyash or slag and pre-desiliconization with the volume ratio (liter) of sodium hydroxide solution, must pre-desiliconization slurries after 1.0～4.0 hours 70～100 ℃ of pre-desiliconizations of following constant temperature;
By flyash or the pre-desilication process of slag, improved the alumina silica ratio in the concentrate, promoted the taste of flyash or slag as bauxite resource, extract aluminum oxide for flyash or slag utilization and opened up new road, and greatly reduced flyash or slag and extracted the waste residue amount that produces behind the aluminum oxide, compare directly and extract the output that aluminum and coproducing cement has significantly reduced cement, reduced the waste residue intractability with flyash or slag.
Step B: solid-liquid separation and filter cake washing: pre-desiliconization slurries solid-liquid separation, liquid portion is pre-desiliconization filtrate, and solid part is a filter cake;
With 50～85 ℃ water wash filter cake, the volume of every kilogram of dried used hot water of filter cake is 0.5 liter, and with the filtrate collection behind the drip washing first time filter cake, merging the back together with pre-desiliconization filtrate after pre-desiliconization slurries separate is pre-desiliconization dope;
Continue to circulate with hot sodium hydroxide solution or hot water drip washing filter cake: the temperature of hot water or hot sodium hydroxide solution is 50～85 ℃, the mass percent concentration of sodium hydroxide solution is lower than 20%, the volume (liter) of the quality of filter cake (kilogram) and hot sodium hydroxide solution or hot water is than being 1: 0.5, since drip washing second time filter cake, filtrate behind the once washing filter cake of back is gone as the previous washing diluted sodium hydroxide solution of next round at every turn, by that analogy, to the last the content of sodium oxide and silicon-dioxide roughly merges itself and pre-desiliconization dope after quite in the filtrate behind the once washing and the pre-desiliconization dope, the raw material that divides the preparation white carbon black as carbon, changing other hot sodium hydroxide solution or hot water again continues filter cake is washed, the quality percentage composition of sodium oxide is lower than 8.8% in filter cake, stops filter cake washing;
Through the oven dry of the filter cake after the washing, be concentrate, the aluminum oxide of concentrate and the mass ratio of silicon oxide are 1.4: 1～1.6: 1;
Step C: the preparation of causticization slag: carry out obtaining being the white carbon black slurries after carbon branch, the ageing after the filtrate merging with pre-desiliconization dope and last washing leaching cake; After the white carbon black slurries solid-liquid separation after the ageing, collecting filtrate is pre-desiliconization mother liquor; Pre-desiliconization mother liquor goes causticization: promptly according to the mol ratio calcium oxide: sodium oxide is to carry out proportioning in 1: 1.1～1: 1.3, and lime is directly added in the pre-desiliconization mother liquor, after 1～2 hour, carries out solid-liquid separation at 95 ℃ of left and right sides stirring reactions, and solid filter cake is the causticization slag;
Step D: with described concentrate, yellow soda ash, also comprise in these the two kinds of materials of causticization slag after lime or the pre-desiliconization mother liquor causticization one or both, according to mol ratio Ca: Si=1.9～2.5, mol ratio Na: (Al+Fe)=0.95～1.05 carry out proportioning, dry grind, be behind the mixing raw material;
Step e: described raw material are carried out sintering under 1100～1250 ℃, and constant temperature 15～120 minutes, it is to be grog about the 60-100 order that the cooling back is crushed to granularity with ball mill;
Step F: described grog and sodium carbonate solution are carried out stripping, the volume of the sodium carbonate solution that the required stripping of per kilogram grog that sinters is used is 3 liters～15 liters, the sodium carbonate solution mass percent concentration is 4%～8%, and stripping is 15～60 minutes in 75 ℃～95 ℃ constant temperature;
Step G: with the solid-liquid separation after the stripping, filtrate collection, solid are filter cake; With 50～85 ℃ pure water drip washing filter cake, every kilogram of used pure water of dried filter cake is 0.5 liter, the filtrate after filtrate collection behind the drip washing first time filter cake and the grog stripping slurries separated and collected is merged the back together be crude liquor of sodium aluminate;
Step H: continue to repeat with 50～85 ℃ white carbon black one wash water or white carbon black two wash water drip washing filter cakes (water when white carbon black one wash water and white carbon black two wash waters are not enough), the volume of every kilogram of dried used liquid of filter cake is with for the first time identical, filtrate behind the once washing filter cake of back is gone as the previous pouring scouring water of next round at every turn, in this washings and crude liquor of sodium aluminate sodium oxide and alumina content roughly quite after, with the filtrate collection after this washing, and merge deep desilication with crude liquor of sodium aluminate; Change other white carbon black one wash water and white carbon black two wash waters or hot water at last again and continue filter cake is washed, the sodium oxide mass percentage content is lower than 7% in white clay, stops washing;
Step I: the processing condition of described crude liquor of sodium aluminate deep desilication are: crude liquor of sodium aluminate adds calcium oxide according to the amount of 6～9 grams per liters, crude liquor of sodium aluminate is placed in the autoclave of sealing, keep mixing speed at 100～200 rev/mins, keep 140～160 ℃ of homo(io)thermism, react after 2 hours, the sodium aluminate filtrate that obtains is seminal fluid, and the siliceous modulus of this seminal fluid is greater than 400;
Step J: Wingdale kiln gas is imported after purifying, sodium aluminate concentrate solution is carried out carbonating decompose, get aluminium hydroxide;
Step K:, get aluminum oxide with aluminium hydroxide roasting down about 1050～1100 ℃.
Present method is extracted aluminum oxide with rational step from flyash or slag, both widened the source channel of aluminum oxide, alleviate the disparities between supply and demand of China's aluminum oxide to a certain extent, can save bauxite resource again, containment China bauxite resource quickens exhausted trend, and can remedy the deficiency of western China bauxite resource, and change the unbalanced Distribution Pattern of China's bauxite resource, greatly alleviated the shortage of China's bauxite resource.
Further, the method for co-producing white carbon black is:
In step C, the filtrate of pre-desiliconization dope and last washing leaching cake is merged, and carbon divided 2～3 hours in 60～95 ℃ of constant temperature, the control carbon dioxide flow, used carbonic acid gas body is 30～99% by long-pending fractional concentration, is carbon minute terminal point in the pH of aforesaid liquid value at 7.5～10.5 o'clock;
50～75 ℃ of following ageings is the white carbon black slurries after 15～60 minutes;
With the white carbon black slurries solid-liquid separation after the ageing; Collecting filtrate is pre-desiliconization mother liquor; Solid is a filter cake;
Pre-desiliconization mother liquor goes causticization: promptly according to the mol ratio calcium oxide: sodium oxide is to carry out proportioning in 1: 1.1～1: 1.3, lime is directly added in the pre-desiliconization mother liquor, at 95 ℃ of stirring reactions after 1～2 hour, carry out solid-liquid separation, solid filter cake is the causticization slag, main component is a lime carbonate, and filtrate is pre-desiliconization circulating mother liquor, directly as pre-desiliconization sodium hydroxide solution;
With 50～85 ℃ water wash filter cake, every kilogram of moisture filter cake need be used the 3-5 premium on currency, and filtrate collection is white carbon black one wash water, white carbon black one wash water, and usefulness in concentrate washing or white clay washing, filter cake is the white carbon black work in-process;
White carbon black work in-process process adds the hydrochloric acid of 2 mol or the sulfuric acid agitator treating of 2 mol purifies, washes the pH value with water between 5～8 then, filtrate collection after the washing is that white carbon black two wash waters are used in the white clay washing, the washing baking oven inner drying of white carbon black under 105～150 ℃ later, being controlled at time of drying after 1～3 hour is the white carbon black finished product.
Further, the method for jointly producing cement is:
In step H,, be white clay through the oven dry of the filter cake after the washing; According to quality than white clay: the ratio batching of lime=5: 1～1: 1 enters the manufacture of cement operation and produces cement.
The present invention improves in the following areas:
1, before pre-desilication reaction, adds a flotation unit, realized making full use of of device.
2, organically continuously the ferric oxide in stage-by-stage extraction flyash or the slag, the whole system technical process of floating pearl, silicon-dioxide and aluminum oxide;
3, the pre-desiliconization of flyash or slag, alumina silica ratio in the concentrate after raising flyash or the pre-desiliconization of slag;
4, after the pre-desiliconization carbon mother liquid causticization in its solution the NaOH mass percent concentration at 10-16%, can directly be used to pre-desiliconization, need not concentrate fully, greatly cut down the consumption of energy, compare the pre-desiliconization technology of other flyash or slag, from white carbon black, extract one ton of white carbon black, approximately can reduce by 3 tons of standard coals/ton white carbon black energy consumption;
5, the optimization of concentrate raw material sintering prescription and sintering process condition not only makes energy consumption reduce, and (solubility rate is meant useful component Na in the concentrate also to have improved solubility rate
2O and AL
2O
3The amount that stripping comes in process in leaching is a call general in the alumina industry);
6, sintered clinker dissolving-out process condition has improved solubility rate;
7, the separation of concentrate, circulation cleaning technology;
8, crude sodium aluminate liquid deep desilication technology, energy consumption has been saved in repeatedly desiliconization;
9, cement is produced in the white clay coproduction.
Beneficial effect of the present invention is: just added a flotation and float the facility of pearl before desilication reaction, can greatly improve the utilization ratio of device.
[description of drawings]
Fig. 1 floats the schema of pearl for the present invention extracts.
[embodiment]
In order to make those skilled in the art can further understand feature of the present invention and technology contents, see also following about detailed description of the present invention and accompanying drawing, accompanying drawing only provide with reference to and explanation, be not to be used for limiting the present invention.
Below in conjunction with accompanying drawing, embodiments of the present invention are described.
As shown in Figure 1, when pearl is floated in extraction from flyash or slag, can realize by following steps:
101: slag is ground, after from dry powder coal ash or slag, magneticly electing smart iron sand, according to solid-to-liquid ratio: i.e. flyash or slag quality (kilogram) and pre-desiliconization is to carry out proportioning in 1: 1.6～1: 8 with the volume ratio (liter) of sodium hydroxide solution, and the adding mass percent is 10%～40% NaOH solution; Normal temperature starts whipping device down, and rotating speed keeps rotating 2～10 minutes at 20～50 rev/mins;
102: after treating to float floating matter on the liquid level, the unlatching floatation equipment will float to be collected in the dashpot after pearl is chosen.
103:, and just can obtain the white pearl product that floats through sorting once more, washing through the de-carbon operation.
In step 101, the step that magneticly elects smart iron sand from dry powder coal ash or slag is:
At first with agitating ball mill with slag mesh-of-grind to 200～250 orders;
Slag after flyash or the grinding carries out magnetic separation with dry-type magnetic extractor, and magneticstrength is 1100～1300 oersteds, just can obtain the crude iron washed ore;
The crude iron washed ore is through taking off the magnetic machine demagnetization;
900～1050 oersteds carry out can obtaining smart iron sand after the magnetic separation.
After pearl was floated in extraction from flyash or slag, this flow process was proceeded, coproduction aluminum oxide, white carbon black and cement raw material:
104: extraction is floated the molten slurries of flyash behind the pearl or slag and sodium hydroxide 70～100 ℃ of pre-desiliconizations of following constant temperature after 1.0～4.0 hours, pre-desiliconization slurries;
105: pre-desiliconization slurries solid-liquid separation, liquid portion is pre-desiliconization filtrate, and solid part is a filter cake, with 50～85 ℃ water wash filter cake; Solid-to-liquid ratio (down with), promptly the volume (every liter) of filter cake quality (every kilogram of dry product) and institute's water is than being 1: 0.5; With the filtrate collection behind the drip washing first time filter cake, merge afterwards standby together with the filtrate after pre-desiliconization slurries separate for pre-desiliconization dope, 50～85 ℃ the mass percent concentration that continues usefulness is lower than 20% diluted sodium hydroxide solution or hot water drip washing filter cake, solid-to-liquid ratio still is 1: 0.5, filtrate behind the once washing filter cake of back is gone as the previous washing diluted sodium hydroxide solution of next round at every turn, such as the diluted sodium hydroxide solution that will use as next round drip washing for the first time filter cake behind the filtrate collection after the secondary washing, wash the diluted sodium hydroxide solution of usefulness for the second time as next round behind the filtrate collection after the washing for the third time, and the like, to the last the content of sodium oxide and silicon-dioxide roughly merges itself and pre-desiliconization dope after quite in the filtrate behind the once washing and the pre-desiliconization dope, the raw material that divides the preparation white carbon black as carbon, changing other hot sodium hydroxide solution or hot water again continues filter cake is washed, the quality percentage composition of sodium oxide is lower than 8.8% in filter cake, stops filter cake washing; Through the oven dry of the filter cake after the washing, be concentrate, the aluminum oxide of concentrate and the mass ratio of silicon oxide are 1.4: 1～1.6: 1, are used as the bauxite resource of soda-lime (stone) sintering process.
106: with the filtrate after pre-desiliconization dope and the last washing, carbon divided 2～3 hours in 60～95 ℃ of constant temperature, the control carbon dioxide flow, used gas concentration lwevel 30～99% (volume fraction) was carbon minute terminal point in the pH of aforesaid liquid value at 7.5～10.5 o'clock;
Aforesaid liquid 50～75 ℃ of following ageings (ageing be meant reaction finish after with the material precipitation fully after, allow the precipitation that just generates place for some time with mother liquor, this process is called " ageing ") be the white carbon black slurries after 15～60 minutes;
107: with the white carbon black slurries solid-liquid separation after the ageing, collecting filtrate is pre-desiliconization mother liquor, and solid is a filter cake;
Pre-desiliconization mother liquor goes causticization, and promptly according to the mol ratio calcium oxide: sodium oxide is to carry out proportioning in 1: 1.1～1: 1.3, and lime is directly added in the pre-desiliconization mother liquor, at 95 ℃ of stirring reactions after 1～2 hour, carry out solid-liquid separation, solid filter cake is the causticization slag, and main component is a lime carbonate; Filtrate is pre-desiliconization circulating mother liquor, and (ultimate principle of causticizing reaction is shown in the following reaction equation to required sodium hydroxide solution: CaO+H during directly as pre-desiliconization
2O=Ca (OH)
2, Na
2CO
3+ Ca (OH)
2=2NaOH+CaCO
3↓, NaHCO
3+ Ca (OH)
2=NaOH+CaCO
3↓+H
2O);
With 50～85 ℃ water wash filter cake of solid-to-liquid ratio 1: 3～1: 5 (quality of moisture filter cake and the volume ratio of bath water), promptly the moisture filter cake of per kilogram need be used the 3-5 premium on currency; Filtrate collection be white carbon black one wash water standby (this filtrate can be used for washing filter cakes behind the pre-desilication reaction, also can be used for subsequent oxidation aluminium produce in the washing of white clay), filter cake is the white carbon black work in-process;
White carbon black work in-process (filter cake) process adds the hydrochloric acid of 2 mol or the sulfuric acid agitator treating of 2 mol purifies, washes the pH value with water 5～8 then, filtrate collection after the washing is white carbon black two wash waters, be used for the washing of alumina producing white clay, the washing baking oven inner drying of white carbon black under 105～150 ℃ later, being controlled at time of drying after 1～3 hour is the white carbon black finished product, and its physico-chemical property is: the DBP absorption value is greater than 2.32cm
3/ g, nitrogen adsorption specific surface area are greater than 190m
2/ g, pH value are 5.3～7.9, weight loss on heating is 4.1%～7.4%;
108: with concentrate, yellow soda ash, and in these the two kinds of materials of causticization slag after lime or the pre-desiliconization mother liquor causticization one or both, according to Ca: Si (being called for short the calcium ratio) is 1.9～2.5 (mol ratios), Na: (Al+Fe) (being called for short the alkali ratio) is that 0.95～1.05 (mol ratio) proportioning is dry grinded, mixing is raw material; Raw material are carried out sintering at 1100～1250 ℃, and constant temperature 15～120 minutes, it is that 60～100 orders are standby sintered clinker that the cooling back is crushed to granularity with ball mill;
109: with the grog that sinters, the volume ratio of the sodium carbonate solution of using according to clinker quality that sinters and stripping (quality is by every kilogram, and volume is by every liter) is 1: 3～1: 15, and the interpolation mass percent is 4%～8%Na
2CO
3Solution, stripping is 15～60 minutes in 75 ℃～95 ℃ constant temperature;
110: with the solid-liquid separation after the stripping, filtrate collection, solid filter cake be with 50-85 ℃ water wash, and the volume (liter) of filter cake quality (per kilogram dry product) and institute's water is than being 1: 0.5;
With the filtrate collection behind the drip washing first time filter cake, merge the back together with filtrate after grog stripping slurries separate and be crude liquor of sodium aluminate;
Continue circulation with 1: 0.5 white carbon black one wash water of solid-to-liquid ratio or white carbon black two wash waters (or water, promptly water replenishes when the white carbon black wash water is not enough) 50-85 ℃ of water wash filter cake, filtrate behind the once washing filter cake of back is gone as the previous washing liquid of next round at every turn, such as the washing lotion that will use as next round drip washing for the first time filter cake behind the filtrate collection after the secondary washing, wash the washing lotion of usefulness for the third time behind the filtrate collection after the washing for the second time as next round, and the like, to the last in filtrate behind the once washing and the crude liquor of sodium aluminate sodium oxide and alumina content roughly quite after, with the filtrate collection behind the last washing leaching cake, and merge with crude liquor of sodium aluminate, come along deep desilication; Change other white carbon black one wash water and white carbon black two wash waters or hot water at last again and continue filter cake is washed, the sodium oxide mass percentage content is lower than 7% in white clay, stops washing; Through the filter cake oven dry after the washing, for white clay standby.
111: the filtrate behind crude liquor of sodium aluminate and the last washing leaching cake together, amount according to 6～9 grams per liters adds calcium oxide, be placed in the autoclave of sealing, keep mixing speed at 100～200 rev/mins, keep 140～160 ℃ of homo(io)thermism, react after 2 hours, the liquid that obtains is seminal fluid, and the siliceous modulus of this seminal fluid is greater than 400 (siliceous modulus is meant the ratio of mass concentration with the mass concentration of silicon of aluminum oxide);
112: (flue gas cleaning is that sintering process is produced method in common in the aluminum oxide, generally makes its dustiness reduce to 0.03g/m by modes such as electrostatic precipitations after purifying with Wingdale kiln gas
3) import sodium aluminate concentrate solution is carried out the carbonating decomposition, get aluminium hydroxide;
113: aluminium hydroxide 1050～1100 ℃ of following roastings, is got aluminum oxide, its impurity component: the mass percent of silicon oxide＜0.04%, sodium oxide mass percent＜0.65%;
114: according to white clay: the mass ratio of lime is 5: 1～1: 1 a ratio batching, enters the manufacture of cement operation and produces cement.
Below tabulation is 11 embodiment according to above flow process, and each embodiment has listed the data of the processing condition in above-mentioned flow process, and the quantum of output of floating pearl and other coproduction products.
Illustrate: latter two embodiment is a feather weight.
By above embodiment as can be seen, present method also realizes flyash or slag resource utilization, minimizing, substep has been chosen ferric oxide in flyash or the slag, has been floated pearl, white carbon black and aluminum oxide have been extracted, and, greatly improve the added value of flyash or slag deep processing with residue white clay utilization production cement;
Present method has also adapted to national Economic development new strategy, from flyash or slag, extract continuously ferric oxide, float that materials such as water, carbonic acid gas, caustic soda, soda ash all can be recycled in the whole technological process of pearl, silicon-dioxide and metallurgical-grade aluminum oxide, energy consumption and material consumption are significantly reduced.For the west area that water resources lacks relatively, the saving of water resources has more importantly meaning undoubtedly.In addition, the discharging of no poisonous, harmful waste does not produce new pollution in the whole technological process, meets the requirement that recycling economy is set up in national Eleventh-Five Year Plan fully, realize the cleaner production that flyash or slag utilize, embodied the perfect unity of environmental benefit, ecological benefits and social benefit.
The above only is embodiments of the present invention, be not so promptly limit claim of the present invention, the equivalent transformation that every utilization specification sheets of the present invention and accompanying drawing content are done directly or indirectly is used in other relevant technical field, all in like manner is included in the claim of the present invention.
Claims (7)
1. one kind is extracted the method for floating pearl from flyash or slag, may further comprise the steps:
Step 1: slag is ground, from dry powder coal ash or slag, magneticly elect smart iron sand after, stir after adding sodium hydroxide solution;
Step 2: after treating to float floating matter on the liquid level, the unlatching floatation equipment will float to be collected in the dashpot after pearl is chosen;
Step 3:, and just can obtain the white pearl product that floats through sorting once more, washing through the de-carbon operation.
2. a kind of method as claimed in claim 1, it is characterized in that, in step 1, the concentration of described sodium hydroxide solution and amount are: mass percent is 10%～40% NaOH solution, and according to solid-to-liquid ratio: i.e. flyash or slag quality (kilogram) and pre-desiliconization is to carry out proportioning in 1: 1.6～1: 8 with the volume ratio (liter) of sodium hydroxide solution.
3. a kind of method as claimed in claim 1 is characterized in that, in step 1, the processing condition of described stirring are: normal temperature starts whipping device down, and rotating speed keeps rotating 2～10 minutes at 20～50 rev/mins.
4. a kind of method as claimed in claim 1 is characterized in that, the method for flyash or slag coproduction ferric oxide is, in step 1:
At first with agitating ball mill with slag mesh-of-grind to 200～250 orders;
Slag after flyash or the grinding carries out magnetic separation with dry-type magnetic extractor, and magneticstrength is 1100～1300 oersteds, just can obtain the crude iron washed ore;
The crude iron washed ore is through taking off the magnetic machine demagnetization;
Pass through the one-level magnetic plant again, magneticstrength is 900～1050 oersteds, carries out can obtaining smart iron sand after the magnetic separation.
5. a kind of method as claimed in claim 1 is characterized in that, flyash or slag coproduction method of alumina are that after pearl was floated in extraction, flyash or slag carried out following steps with the slurries of sodium hydroxide solution:
Steps A: pre-desiliconization: the concentration and the amount that add sodium hydroxide solution in flyash or the slag are, mass percent is between 10%～40%, is to carry out proportioning in 1: 1.6～1: 8 according to the quality (kilogram) of flyash or slag and pre-desiliconization with the volume ratio (liter) of sodium hydroxide solution, must pre-desiliconization slurries after 1.0～4.0 hours 70～100 ℃ of pre-desiliconizations of following constant temperature;
Step B: solid-liquid separation and filter cake washing: pre-desiliconization slurries solid-liquid separation, liquid portion is pre-desiliconization filtrate, and solid part is a filter cake;
With 50～85 ℃ water wash filter cake, the volume of every kilogram of dried used hot water of filter cake is 0.5 liter, and with the filtrate collection behind the drip washing first time filter cake, merging the back together with pre-desiliconization filtrate after pre-desiliconization slurries separate is pre-desiliconization dope;
Continue to circulate with hot sodium hydroxide solution or hot water drip washing filter cake: the temperature of hot water or hot sodium hydroxide solution is 50～85 ℃, the mass percent concentration of sodium hydroxide solution is lower than 20%, the volume (liter) of the quality of filter cake (kilogram) and hot sodium hydroxide solution or hot water is than being 1: 0.5, since drip washing second time filter cake, filtrate behind the once washing filter cake of back is gone as the previous washing diluted sodium hydroxide solution of next round at every turn, by that analogy, to the last the content of sodium oxide and silicon-dioxide roughly merges itself and pre-desiliconization dope after quite in the filtrate behind the once washing and the pre-desiliconization dope, the raw material that divides the preparation white carbon black as carbon, changing other hot sodium hydroxide solution or hot water again continues filter cake is washed, the quality percentage composition of sodium oxide is lower than 8.8% in filter cake, stops filter cake washing;
Through the oven dry of the filter cake after the washing, be concentrate, the quality of the aluminum oxide of concentrate and the mass ratio of silicon oxide are 1.4: 1～1.6: 1;
Step C: the preparation of causticization slag: carry out obtaining being the white carbon black slurries after carbon branch, the ageing after the filtrate merging with pre-desiliconization dope and last washing leaching cake; After the white carbon black slurries solid-liquid separation after the ageing, collecting filtrate is pre-desiliconization mother liquor; Pre-desiliconization mother liquor goes causticization: promptly according to the mol ratio calcium oxide: sodium oxide is to carry out proportioning in 1: 1.1～1: 1.3, and lime is directly added in the pre-desiliconization mother liquor, after 1～2 hour, carries out solid-liquid separation at 95 ℃ of left and right sides stirring reactions, and solid filter cake is the causticization slag;
Step D: with described concentrate, yellow soda ash, also comprise in these the two kinds of materials of causticization slag after lime or the pre-desiliconization mother liquor causticization one or both, according to mol ratio Ca: Si=1.9～2.5, mol ratio Na: (Al+Fe)=0.95～1.05 carry out proportioning, dry grind, be behind the mixing raw material;
Step e: described raw material are carried out sintering under 1100～1250 ℃, and constant temperature 15～120 minutes, it is to be grog about 60～100 orders that the cooling back is crushed to granularity with ball mill;
Step F: described grog and sodium carbonate solution are carried out stripping, the volume of the sodium carbonate solution that the required stripping of per kilogram grog that sinters is used is 3 liters～15 liters, the sodium carbonate solution mass percent concentration is 4%～8%, and stripping is 15～60 minutes in 75 ℃～95 ℃ constant temperature;
Step G: with the solid-liquid separation after the stripping, filtrate collection, solid are filter cake; With 50～85 ℃ pure water drip washing filter cake, every kilogram of used pure water of dried filter cake is 0.5 liter, the filtrate after filtrate collection behind the drip washing first time filter cake and the grog stripping slurries separated and collected is merged the back together be crude liquor of sodium aluminate;
Step H: continue to repeat with 50～85 ℃ white carbon black one wash water or white carbon black two wash water drip washing filter cakes (water when white carbon black one wash water and white carbon black two wash waters are not enough), the volume of every kilogram of dried used liquid of filter cake is with for the first time identical, filtrate behind the once washing filter cake of back is gone as the previous pouring scouring water of next round at every turn, in this washings and crude liquor of sodium aluminate sodium oxide and alumina content roughly quite after, with the filtrate collection after this washing, and merge deep desilication with crude liquor of sodium aluminate; Change other white carbon black one wash water and white carbon black two wash waters or hot water at last again and continue filter cake is washed, the mass percentage content of sodium oxide is lower than 7% in white clay, stops washing;
Step I: the processing condition of described crude liquor of sodium aluminate deep desilication are: crude liquor of sodium aluminate adds calcium oxide according to the amount of 6～9 grams per liters, crude liquor of sodium aluminate is placed in the autoclave of sealing, keep mixing speed at 100～200 rev/mins, keep 140～160 ℃ of homo(io)thermism, react after 2 hours, the sodium aluminate filtrate that obtains is seminal fluid, and the siliceous modulus of this seminal fluid is greater than 400;
Step J: Wingdale kiln gas is imported after purifying, sodium aluminate concentrate solution is carried out carbonating decompose, get aluminium hydroxide;
Step K:, get aluminum oxide with aluminium hydroxide roasting down about 1050～1100 ℃.
6. a kind of method as claimed in claim 5 is characterized in that, the method for co-producing white carbon black is:
In step C, the filtrate of pre-desiliconization dope and last washing leaching cake is merged, and carbon divided 2～3 hours in 60～95 ℃ of constant temperature, the control carbon dioxide flow, used carbonic acid gas body is 30～99% by long-pending fractional concentration, is carbon minute terminal point in the pH of aforesaid liquid value at 7.5～10.5 o'clock;
50～75 ℃ of following ageings is the white carbon black slurries after 15～60 minutes;
With the white carbon black slurries solid-liquid separation after the ageing; Collecting filtrate is pre-desiliconization mother liquor; Solid is a filter cake;
Pre-desiliconization mother liquor goes causticization: promptly according to the mol ratio calcium oxide: sodium oxide is to carry out proportioning in 1: 1.1～1: 1.3, lime is directly added in the pre-desiliconization mother liquor, at 95 ℃ of stirring reactions after 1～2 hour, carry out solid-liquid separation, solid filter cake is the causticization slag, main component is a lime carbonate, and filtrate is pre-desiliconization circulating mother liquor, directly as pre-desiliconization sodium hydroxide solution;
With 50～85 ℃ water wash filter cake, every kilogram of moisture filter cake need be with 3～5 premium on currency, and filtrate collection is white carbon black one wash water, white carbon black one wash water, and usefulness in concentrate washing or white clay washing, filter cake is the white carbon black work in-process;
White carbon black work in-process process adds the hydrochloric acid of 2 mol or the sulfuric acid agitator treating of 2 mol purifies, washes the pH value with water between 5～8 then, filtrate collection after the washing is that white carbon black two wash waters are used in the white clay washing, the washing baking oven inner drying of white carbon black under 105～150 ℃ later, being controlled at time of drying after 1～3 hour is the white carbon black finished product.
7. a kind of method as claimed in claim 5 is characterized in that, the method for jointly producing cement is:
In step H,, be white clay through the oven dry of the filter cake after the washing; According to quality than white clay: the ratio batching of lime=5: 1～1: 1 enters the manufacture of cement operation and produces cement.
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